Photothermal cracking hydrogen production reactor

Abstract

The utility model relates to the technical field of hydrogen production equipment, and discloses a photo-thermal cracking hydrogen production reactor which comprises a shell and a reaction cavity, a light-transmitting plate is arranged at the front end of the shell, and a metal oxide catalysis component is arranged in the reaction cavity; a water inlet pipe is arranged on the side face of the shell. An exhaust pipe is arranged at the rear end of the shell. When the interior of the reaction cavity is in a reduction reaction temperature state, the metal oxide catalysis assembly is subjected to a reduction reaction to separate out oxygen, and the oxygen is exhausted through the exhaust pipe; when the interior of the reaction cavity is in an oxidation reaction temperature state, quantitative water is injected into the reaction cavity from the water inlet pipe, the water and the metal oxide catalysis assembly subjected to the reduction reaction are subjected to oxidation reaction to separate out hydrogen, and the hydrogen is exhausted through the exhaust pipe. According to the device, hydrogen is produced through two-step reaction, and the metal oxide catalysis assembly is free of consumption and can be continuously used.

Description

Technical Field

[0001] The utility model relates to the technical field of hydrogen production equipment, in particular to a photothermal cracking hydrogen production reactor. Background Art

[0002] Hydrogen energy has broad prospects as clean electricity and is also an effective form of electricity storage. Hydrogen production from traditional energy sources such as coal and natural gas is still the main way, accounting for 99%. The hydrogen produced is called gray hydrogen or blue hydrogen, while hydrogen produced from clean energy is called green hydrogen, accounting for only about 1%.

[0003] The current green hydrogen manufacturing technology is mainly the water electrolysis process. The water electrolysis process route uses secondary energy to produce hydrogen, which still has a carbon footprint and is relatively expensive. Direct high-temperature pyrolysis to produce hydrogen requires heating water to above 3000°C to decompose part of the water vapor into hydrogen and oxygen. The energy consumption is very large and the cost is also high, making it difficult to promote and use. Therefore, how to produce green hydrogen at a lower cost and energy consumption is the key and difficulty of hydrogen production. Utility Model Content

[0004] In order to solve the above problems existing in the prior art, the utility model provides a photothermal cracking hydrogen production reactor which is clean, pollution-free, low in energy consumption and long in service life.

[0005] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0006] A photothermal cracking hydrogen production reactor comprises a shell and a reaction chamber arranged in the shell, wherein a light-transmitting plate for concentrated sunlight to be incident into the reaction chamber is arranged at the front end of the shell, and a metal oxide catalyst component with a microporous structure is arranged in the reaction chamber; a water inlet pipe is arranged on the side of the shell, and an exhaust pipe is arranged at the rear end of the shell;

[0007] The temperature in the reaction chamber is adjusted by changing the light intensity entering the reaction chamber, so that the temperature in the reaction chamber forms a reduction reaction temperature and an oxidation reaction temperature that alternately change according to a preset cycle; when the reaction chamber is at the reduction reaction temperature state, the metal oxide catalytic component undergoes a reduction reaction to precipitate oxygen and discharges the oxygen through the exhaust pipe; when the reaction chamber is at the oxidation reaction temperature state, a certain amount of water is injected into the reaction chamber from the water inlet pipe, and the water undergoes an oxidation reaction with the metal oxide catalytic component after the reduction reaction to precipitate hydrogen and discharge the hydrogen through the exhaust pipe.

[0008] Preferably, the metal oxide catalyst assembly includes a catalyst core disposed in a tubular catalyst body and coaxially disposed in the tubular catalyst body, the catalyst core is in a conical structure, the small diameter end of the catalyst core faces the light-transmitting plate, and the reaction chamber is disposed in the tubular catalyst body. The tubular catalyst body covers the reaction chamber, and the catalyst core is disposed in the reaction chamber, thereby increasing the contact surface area between the metal oxide catalyst assembly and the reaction chamber and improving the reaction efficiency.

[0009] Preferably, the inner hole of the tubular catalyst body is a tapered hole that is small in the front and large in the back, and a tapered transition surface is provided at the front end of the tapered hole, and the front end of the tapered transition surface expands outward to form a tapered expansion hole, and the light-transmitting plate is fixed at the large-diameter end of the tapered expansion hole. The tapered expansion hole allows light from all angles to enter the reaction chamber, thereby increasing the energy density in the reaction chamber; the tapered transition surface and the tapered hole can effectively prevent the light entering the reaction chamber from being reflected, thereby reducing heat loss and improving the light-heat utilization rate.

[0010] Preferably, the tubular catalyst body and the catalyst core are both provided with a plurality of annularly distributed gas release channels, which are conducive to the release of oxygen and hydrogen.

[0011] Preferably, a gas channel is provided at the center of the catalytic core, and the exhaust pipe includes an oxygen pipe and a hydrogen pipe sleeved outside the oxygen pipe, and the oxygen pipe and the hydrogen pipe are both connected to the rear end of the gas channel.

[0012] Preferably, the reduction reaction temperature is configured to be 1500-2000°C, and the oxidation reaction temperature is configured to be 1150-1350°C.

[0013] Preferably, the inner end of the water inlet pipe extends into the tubular catalyst body and communicates with the reaction chamber through micropores, and the pore gap of the micropores is configured to be 50-1500 μm. The water at the outlet of the water inlet pipe is directly vaporized into water vapor at high temperature, and the water vapor penetrates into the micropores of the tubular catalyst body under pressure, thereby greatly improving the reaction efficiency.

[0014] Preferably, a heat-insulating cup is disposed outside the tubular catalyst body, and a closed annular heat-insulating cavity is formed between the heat-insulating cup and the shell. The heat-insulating cup can reduce heat loss and improve heat utilization.

[0015] Preferably, a buffer support ring is provided in the annular heat insulation cavity, which plays a supporting role on the one hand and a buffering role on the other hand to thermal expansion and contraction.

[0016] Preferably, a mounting seat is provided at the bottom of the housing, which facilitates installation.

[0017] Therefore, the utility model uses a metal oxide catalytic component to carry out reduction reaction and oxidation reaction in a reaction chamber in an alternating cycle, and splits water into hydrogen in two steps at high temperature, thereby reducing the temperature required for the reaction and improving the reaction efficiency; at the same time, the reactions are carried out alternately, the metal oxide catalytic component has no consumption, can be used continuously, has a long service life, and has a low maintenance cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 It is a structural schematic diagram of the utility model.

[0019] Figure 2 for Figure 1 Another perspective of the picture.

[0020] Figure 3 It is a schematic diagram of the internal structure of the utility model.

[0021] Figure 4 This is a usage state diagram of the utility model.

[0022] In the figure: shell 1, reaction chamber 2, light-transmitting plate 3, metal oxide catalyst assembly 4, tubular catalyst body 40, gas precipitation channel 400, tapered hole 401, tapered transition surface 402, tapered expansion hole 403, catalyst core 41, gas channel 410, water inlet pipe 5, exhaust pipe 6, oxygen pipe 60, hydrogen pipe 61, insulation cup 7, annular insulation chamber 70, buffer support ring 71, mounting seat 8, bracket 9, dish-type solar concentrator 10. DETAILED DESCRIPTION

[0023] In order to make the technical problems, technical solutions and beneficial technical effects to be solved by the present invention more clearly understood, the present invention will be further described in detail below in conjunction with the accompanying drawings and multiple exemplary embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention, rather than to limit the scope of protection of the present invention.

[0024] It should be understood that, in this document, the expressions "first", "second", etc. are used for descriptive purposes only and should not be understood as indicating or implying relative importance, nor should they be understood as implicitly indicating the number of technical features indicated. Features defined as "first" or "second" may explicitly or implicitly indicate that at least one of the features is included.

[0025] like Figure 1-3 A photothermal cracking hydrogen production reactor shown includes a shell 1 and a reaction chamber 2 arranged in the shell. The front end of the shell 1 is provided with a light-transmitting plate 3 for concentrated sunlight to be injected into the reaction chamber, and the reaction chamber 2 is provided with a metal oxide catalyst component 4 with a microporous structure; a water inlet pipe 5 is provided on the side of the shell 1, and an exhaust pipe 6 is provided at the rear end of the shell; the temperature in the reaction chamber is adjusted by changing the light intensity entering the reaction chamber, so that the temperature in the reaction chamber forms a reduction reaction temperature and an oxidation reaction temperature that alternately change according to a preset cycle; when the reaction chamber is at the reduction reaction temperature state, the metal oxide catalyst component undergoes a reduction reaction to precipitate oxygen and discharges the oxygen through the exhaust pipe; when the reaction chamber is at the oxidation reaction temperature state, a certain amount of water is injected into the reaction chamber at the water inlet pipe, and the water undergoes an oxidation reaction with the metal oxide catalyst component after the reduction reaction to precipitate hydrogen and discharge the hydrogen through the exhaust pipe.

[0026] The material of the metal oxide catalytic component is MxOy, wherein x and y are both natural numbers greater than or equal to 1. In some embodiments, M is configured as a metal element such as Mn, Mg, Cd, Zn, Ce, Fe, Ca, Ti, Mo, Co, etc., then MxOy is MnO2, MgO2, CdO, ZnO2, CeO2, Fe3O4, CaO, TiO2, MoO2, Co3O4, etc.; the metal elements in the above metal oxides are all in a high-valent state; the reduction reaction temperature is configured to 1500-2000°C, and the oxidation reaction temperature is configured to 1150-1350°C. In this embodiment, the reduction reaction temperature is set to 1800°C, and the oxidation reaction temperature is set to 1200°C. The general expression when the reaction chamber is at the reduction reaction temperature is as follows: 2MxOy→2MxO(y-1)+O2↑, that is, the high-valent metal oxide generates a low-valent metal oxide through a reduction reaction and releases oxygen; then a certain amount of water is injected into the reaction chamber, and the water is directly vaporized into water vapor. The general expression when the water vapor and MxO(y-1) undergo an oxidation reaction is: MxO(y-1)+H2O→MxOy+H2↑. Hydrogen and oxygen are discharged through the exhaust pipe and collected.

[0027] like Figure 3 As shown, the metal oxide catalyst assembly 4 includes a catalytic core 41 arranged in a tubular catalyst body 40 and coaxially arranged in the tubular catalyst body. The catalytic core has a conical structure, and the small diameter end of the catalytic core faces the light-transmitting plate. The reaction chamber is arranged in the tubular catalyst body; a gas channel 410 is provided in the center of the catalytic core 41, and the exhaust pipe 6 includes an oxygen pipe 60 and a hydrogen pipe 61 sleeved on the outside of the oxygen pipe, and the oxygen pipe and the hydrogen pipe are both connected to the rear end of the gas channel 410.

[0028] The tubular catalyst body 40 and the catalyst core 41 are both provided with a plurality of annularly distributed gas precipitation channels 400. The inner end of the water inlet pipe 5 extends into the tubular catalyst body 40 and communicates with the reaction chamber through micropores. The inner hole of the tubular catalyst body 40 is a tapered hole 401 that is small in the front and large in the back. The front end of the tapered hole 401 is provided with a tapered transition surface 402. The front end of the tapered transition surface expands outward to form a tapered expansion hole 403. The large diameter end of the tapered transition surface 402 is connected to the front end of the tapered hole. The small diameter end of the tapered transition surface 402 is communicated with the tapered expansion hole 403. The light-transmitting plate 3 is fixedly provided at the large diameter end of the tapered expansion hole. The light-transmitting plate in this embodiment is a quartz light-transmitting plate.

[0029] An insulating cup 7 is disposed outside the tubular catalyst body 40, and a closed annular insulating cavity 70 is formed between the insulating cup 7 and the housing 1. A buffer support ring 71 is disposed inside the annular insulating cavity 70. A mounting seat 8 is disposed at the bottom of the housing 1.

[0030] In conjunction with the accompanying drawings, the principle of the utility model is as follows: Figure 4As shown, the hydrogen production reactor is installed on the dish-type solar concentrator 10 through a bracket 9. The light concentrated on the dish-type solar concentrator passes through the light-transmitting plate into the reaction chamber, so that the temperature in the reaction chamber reaches the temperature of the reduction reaction (about 1800°C). At this time, the metal oxide catalytic component undergoes a reduction reaction at this temperature, and the high-valent metal is oxidized and reduced to a low-valent metal oxide (or metal element), and oxygen is generated at the same time, and the oxygen is discharged through the oxygen pipe; then a certain amount of water is injected into the reaction chamber through the water inlet pipe, and the water absorbs heat and vaporizes and then penetrates into the micropores of the metal oxide catalytic component. By adjusting the dish-type solar concentrator, the light entering the reactor is reduced (that is, the energy density is reduced), and then the temperature in the reaction zone is reduced to the temperature of the oxidation reaction (about 1200°C). At this time, the low-valent metal oxide (or metal element) undergoes an oxidation reaction with water (steam), and the low-valent metal oxide (or metal element) reacts to generate a high-valent metal oxide, while releasing hydrogen, which is discharged through the hydrogen pipe and collected. When the water (steam) in the reaction chamber is reacted, the dish solar concentrator is adjusted again to increase the light entering the reaction chamber, increase the energy density, and return the temperature in the reaction chamber to the reduction reaction temperature, so that the metal oxide catalytic component undergoes a reduction reaction again, and the alternating cycle continues to split water into hydrogen, thereby producing hydrogen. This device produces hydrogen through a two-step reaction, reduces the reaction temperature, and is environmentally friendly and pollution-free. The metal oxide catalytic component has no consumption and can operate stably for a long time. The overall maintenance cost is low, and it has great commercial application prospects.

[0031] In the description of the present invention, it is necessary to understand that the directions or positional relationships indicated by up, down, left, right, inner end, outer end, one end, the other end, etc. are based on the orientations or positional relationships shown in the accompanying drawings, and are only for the purpose of more clearly describing the technical solution of the present invention, rather than indicating or implying that the device or element referred to must have a specific direction, be constructed and operated in a specific orientation, and cannot be understood as a limitation of the present invention.

[0032] Although specific embodiments of the present invention are described in detail herein, they are provided for the purpose of explanation only and should not be considered to limit the scope of the present invention. Various substitutions, changes and modifications may be conceived without departing from the spirit and scope of the present invention.

Claims

1. A photothermal decomposition hydrogen production reactor, Its characteristics are: It comprises a shell and a reaction chamber arranged in the shell, wherein the front end of the shell is provided with a light-transmitting plate for radiating concentrated sunlight into the reaction chamber, and the reaction chamber is provided with a metal oxide catalyst component with a microporous structure; a water inlet pipe is arranged on the side of the shell, and an exhaust pipe is arranged at the rear end of the shell; The temperature in the reaction chamber is adjusted by changing the light intensity entering the reaction chamber, so that the temperature in the reaction chamber forms a reduction reaction temperature and an oxidation reaction temperature that alternately change according to a preset cycle; when the reaction chamber is at the reduction reaction temperature state, the metal oxide catalytic component undergoes a reduction reaction to precipitate oxygen and discharges the oxygen through the exhaust pipe; when the reaction chamber is at the oxidation reaction temperature state, a certain amount of water is injected into the reaction chamber from the water inlet pipe, and the water undergoes an oxidation reaction with the metal oxide catalytic component after the reduction reaction to precipitate hydrogen and discharge the hydrogen through the exhaust pipe.

2. The photothermal decomposition hydrogen production reactor according to claim 1, Its characteristics are: The metal oxide catalyst assembly comprises a catalyst core arranged in a tubular catalyst body and coaxially arranged in the tubular catalyst body. The catalyst core is in a conical structure, and the small diameter end of the catalyst core faces the light-transmitting plate. The reaction chamber is arranged in the tubular catalyst body.

3. The photothermal decomposition hydrogen production reactor according to claim 2, Its characteristics are: The inner hole of the tubular catalyst body is a tapered hole with a small front and a large rear. The front end of the tapered hole is provided with a tapered transition surface, and the front end of the tapered transition surface expands outward to form a tapered expansion hole. The light-transmitting plate is fixedly arranged at the large diameter end of the tapered expansion hole.

4. The photothermal decomposition hydrogen production reactor according to claim 2, Its characteristics are: The tubular catalyst body and the catalyst core are both provided with a plurality of gas precipitation channels distributed in an annular shape.

5. The photothermal decomposition hydrogen production reactor according to claim 2, Its characteristics are: A gas channel is arranged at the center of the catalytic core, and the exhaust pipe comprises an oxygen pipe and a hydrogen pipe sleeved outside the oxygen pipe, and the oxygen pipe and the hydrogen pipe are both connected to the rear end of the gas channel.

6. The photothermal decomposition hydrogen production reactor according to claim 1, Its characteristics are: The reduction reaction temperature is configured to be 1500-2000°C, and the oxidation reaction temperature is configured to be 1150-1350°C.

7. The photothermal decomposition hydrogen production reactor according to claim 2, Its characteristics are: The inner end of the water inlet pipe extends into the tubular catalyst body and communicates with the reaction chamber through micropores, and the pore gap of the micropores is configured to be 50-1500 μm.

8. The photothermal decomposition hydrogen production reactor according to claim 2, Its characteristics are: A heat-insulating cup is arranged on the outer side of the tubular catalyst body, and a closed annular heat-insulating cavity is formed between the heat-insulating cup and the shell.

9. The photothermal decomposition hydrogen production reactor according to claim 8, Its characteristics are: A buffer support ring is arranged in the annular heat insulation cavity.

10. The photothermal decomposition hydrogen production reactor according to claim 1, Its characteristics are: A mounting seat is provided at the bottom of the shell.

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