Solar thermochemical cycle hydrogen production reactor
By using a fluidized bed reactor and catalyst circulation design in solar thermal chemical cyclic hydrogen production, the problem of catalyst sintering at high temperatures is solved, and long-term stable operation and efficient hydrogen production are achieved.
Patent Information
- Application Number
- CN202311164699.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2023-09-11
- Publication Date
- 2025-03-11
AI Technical Summary
During the hydrogen production process of solar thermal chemical cycle, the catalyst is prone to sintering under high temperature conditions, which affects the long-term use of the process.
Using a fluidized bed reactor, the circulating flow and fluidization reaction of the catalyst is realized through the high and low arrangement of the water cracking reactor and the input of the fluidized steam, and the circulating flow and fluidization reaction of the catalyst are avoided from high temperature sintering.
The long-term stable operation of the catalyst is achieved, the sintering phenomenon is avoided, and the sustainability and economic benefits of hydrogen production technology are improved.
Smart Images
Figure CN119588257A_ABST
Abstract
Description
Technical Field
[0001] The invention belongs to the technical field of solar hydrogen production, and in particular relates to a solar thermochemical cycle hydrogen production reactor. Background Art
[0002] Energy and environment are two major themes of today's social development. At present, the main sources of energy are fossil fuels such as coal, natural gas and oil. However, facing problems such as depletion and environmental pollution, researching and developing cheap, efficient, clean and sustainable energy is a great and arduous task for contemporary energy workers. Hydrogen energy, as a clean new energy source, is the most ideal substitute for traditional energy. Hydrogen has the advantages of being clean, pollution-free, storable and having high calorific value. The final product of hydrogen utilization is water, which has zero pollution and zero carbon emissions. Hydrogen obtained from clean energy such as solar energy is completely carbon-free and clean throughout the process. Compared with electric energy, hydrogen can be stored. Compared with other fuels, hydrogen has a higher calorific value, and its mass calorific value is three times that of gasoline. Hydrogen energy is a green energy that can solve both the energy crisis and environmental pollution problems in the future, and is the future direction of energy development.
[0003] Solar hydrogen production is one of the important ways to produce hydrogen from renewable energy, mainly including photovoltaic water electrolysis hydrogen production, photocatalytic hydrogen production, and thermochemical cycle hydrogen production.
[0004] Photovoltaic electrolysis of water to produce hydrogen generates electricity through photovoltaic cells, which then drive the electrolyzer to produce hydrogen. The principle of water electrolysis to produce hydrogen is that water decomposes under power conditions, a reduction reaction occurs at the cathode to precipitate hydrogen, and an oxidation reaction occurs at the anode to produce oxygen. Water electrolysis to produce hydrogen is one of the most mature and widely used hydrogen production technologies. The overall hydrogen production efficiency is about 12.0% to 14.2% (solar silicon cell 20.3% × alkaline electrolytic cell 59% to 70%), and it has now entered the stage of promotion and application. The problem with this technology is that after two steps of wind and solar power generation and electricity production of hydrogen, the energy conversion efficiency of each stage is low, and the electrolyzer technology still needs to continue to develop, so it is not the best way to produce hydrogen.
[0005] Photocatalytic water splitting to produce hydrogen uses high-frequency photons in the solar spectrum to act on photocatalysts to form oxygen vacancies, thereby capturing oxygen atoms from water molecules to produce hydrogen. The selection of visible light catalysts in the process of photocatalytic water splitting to produce hydrogen is crucial. However, most catalysts currently used for photocatalytic water splitting to produce hydrogen have relatively low visible light response and quantum efficiency. Researching and developing high-efficiency, low-cost, and highly stable photocatalysts is a very challenging and significant task. At present, the technology is in its infancy, with a hydrogen production efficiency of about 2.0%, which is not worth commercializing.
[0006] Thermochemical cycle hydrogen production mainly uses the concentrating technology to convert solar energy into high-temperature heat energy to indirectly drive the water decomposition cycle, realizing the high-temperature water cracking hydrogen production reaction. The cracking process is divided into multiple cycle reactions, oxygen is produced in one step, and hydrogen is obtained in another step, which solves the problem of hydrogen and oxygen separation. In recent years, with the rapid development of concentrating and collecting technology, dish-type solar concentrators with high concentration ratio and high collection temperature provide a matching heat source for thermochemical cycle hydrogen production, laying the foundation for the further development of solar high-temperature cracking hydrogen production technology.
[0007] Compared with photovoltaic water electrolysis and photocatalytic water decomposition, solar thermochemical cycle hydrogen production converts full-spectrum solar energy into thermal energy for hydrogen production, so the theoretical efficiency is relatively high (about 50%). However, most current studies use fixed bed reactors. Although scholars have compared hundreds of catalysts, after more than a dozen rounds of oxidation-reduction cycles, the powder catalysts all show sintering. The sintering and aggregation of the powder increases its particle size, which in turn leads to a decrease in the specific surface area of the material. The output of hydrogen produced by water cracking has dropped drastically, and it is basically difficult to reuse.
[0008] In summary, the technology of photocatalytic water splitting to produce hydrogen is not yet mature, the efficiency of hydrogen production is low, and it is still in the laboratory stage. The technology of photovoltaic power generation + water electrolysis to produce hydrogen is mature and has been commercialized on a large scale, but the overall efficiency of hydrogen production is not high, and there are environmental problems in the manufacturing process of photovoltaic cells. Solar thermochemical cycle hydrogen production has high overall efficiency and is the most promising hydrogen production technology, but there is a problem of catalyst sintering under high temperature conditions, which affects the long-term use of this process technology. How to inhibit the sintering of catalyst powder and maintain activity is a key research issue in solar thermochemical cycle hydrogen production. Summary of the invention
[0009] The present invention discloses a solar thermochemical cycle hydrogen production reactor, which is intended to solve the problem of catalyst sintering under high temperature conditions during the process of producing hydrogen using the solar thermochemical cycle, thereby affecting the long-term use of the process technology.
[0010] To solve the above technical problems, the technical solution adopted by the present invention is as follows: a solar thermochemical cycle hydrogen production reactor, comprising: a gas steam pipe, the gas steam pipe is connected to the inlet of a catalyst lifting pipe, a water splitting reactor, the outlet of the catalyst lifting pipe extends into the interior of the water splitting reactor, the stripping steam carries the catalyst through the gas steam pipe and the catalyst lifting pipe in turn into the water splitting reactor, the catalyst in the water splitting reactor undergoes an oxidation reaction under high temperature conditions to generate hydrogen, a catalyst regenerator, the catalyst regenerator is connected to the water splitting reactor through a to-be-regenerated inclined pipe, the catalyst after the reaction in the water splitting reactor flows into the catalyst regenerator through the to-be-regenerated inclined pipe, and undergoes a reduction reaction under high temperature conditions to generate oxygen and regenerated catalyst, the regenerated catalyst acquires activity under the action of oxygen, the catalyst regenerator is connected to a regeneration inclined pipe, one end of the regeneration inclined pipe is connected to the catalyst lifting pipe, the regenerated catalyst sequentially passes through the regeneration inclined pipe and the catalyst lifting pipe into the water splitting reactor for circulation to perform a hydrogen production reaction, and fluidizing steam is introduced into the water splitting reactor and the catalyst regenerator.
[0011] Preferably, a first cyclone separator is provided inside the water splitting reactor, and a second cyclone separator is provided outside the water splitting reactor, the first cyclone separator is connected to the outlet of the catalyst lifting pipe, the first cyclone separator is used to classify the feed catalyst and the stripping steam, and the second cyclone separator is used to separate the hydrogen, water and the carried catalyst at the outlet.
[0012] Preferably, a third cyclone separator is provided outside the catalyst regenerator, and the third cyclone separator is used to separate the reaction product containing oxygen at the outlet and the carried catalyst.
[0013] Preferably, an air distribution plate is provided at the bottom of the water splitting reactor and the catalyst regenerator, a first fluidized steam pipe is connected to the bottom of the water splitting reactor, and a second fluidized steam pipe is connected to the bottom of the catalyst regenerator. The fluidized steam passes through the first fluidized steam pipe or the second fluidized steam pipe and then through the air distribution plate into the water splitting reactor or the catalyst regenerator. The air distribution plate is used for uniform distribution of the fluidized steam.
[0014] Preferably, the first cyclone separator is connected to a first catalyst feed leg, the second cyclone separator is connected to a second catalyst feed leg, the water splitting reactor and the catalyst regenerator both adopt fluidized bed reactors, the first catalyst feed leg or the second catalyst feed leg is used to input the catalyst separated by the first cyclone separator or the second cyclone separator into the bed layer of the fluidized bed of the water splitting reactor, and the third cyclone separator is connected to a third catalyst feed leg, and the third catalyst feed leg is used to input the catalyst separated by the third cyclone separator into the bed layer of the fluidized bed of the catalyst regenerator.
[0015] Preferably, a first quartz glass is provided on the top of the water splitting reactor, and a second quartz glass is provided on the top of the catalyst regenerator, and the first quartz glass and the second quartz glass are used to allow an external heat source to enter the water splitting reactor and the catalyst regenerator through radiation to heat the catalyst and steam.
[0016] Preferably, the second cyclone separator is connected to a first outlet pipe, which is used to transport the gas product of the oxidation reaction to a heat exchanger for subsequent treatment, and the third cyclone separator is connected to a second outlet pipe, which is used to transport the oxygen after the reaction to a heat exchanger for subsequent treatment.
[0017] Preferably, the inner walls of the water splitting reactor and the catalyst regenerator are made of high temperature resistant ceramic materials, and the outer walls of the water splitting reactor and the catalyst regenerator are provided with insulation plates, which are used to prevent heat loss.
[0018] Preferably, the inlets of the fluidizing steam and the stripping steam are both provided with a flow meter and a regulating valve, the flow meter is used to detect the flow value of the fluidizing steam or stripping steam inlet, and the regulating valve is used to adjust the opening of the regulating valve according to the flow required at the first fluidizing steam pipe or the second fluidizing steam pipe or the gas steam pipe.
[0019] Preferably, the water splitting reactor is arranged at a height higher than the catalyst regenerator, the catalyst regenerator is higher than the inlet of the catalyst riser, the catalyst flows from the water splitting reactor to the catalyst regenerator by gravity, the catalyst flows from the catalyst riser to the water splitting reactor by steam gas, and the system pressure is balanced.
[0020] The beneficial effects of the present invention include:
[0021] 1. In the present invention, high-temperature thermal energy generated by focusing clean solar energy is used as the driving heat source. Water undergoes an oxidation-reduction reaction through a catalyst material under high-temperature conditions, and is cracked to produce oxygen and hydrogen, thereby realizing the conversion of low-temperature solar energy into high-quality hydrogen energy.
[0022] 2. In the present invention, by changing the form of reaction, the current fixed bed reaction is changed to a fluidized bed reaction. By setting up two main devices, a water splitting reactor and a catalyst regenerator, and by arranging them high and low, a height difference in material level is generated, which drives the catalyst flow between the two devices, and the reduced catalyst at a low material level is lifted to the water splitting reactor through a catalyst lifting pipe. The above measures realize the circulation of the catalyst. By arranging fluidized steam at the bottom of the water splitting reactor and the catalyst regenerator, a fluidized reaction of the catalyst and the reaction raw materials is realized. The catalyst is in a fluidized state and a gas-solid two-phase flow state during the whole process, and the catalysts move relative to each other. At the same time, under the influence of the fluidized steam, the catalyst will not undergo high-temperature sintering. The system can operate stably for a long period of time, with continuous feeding and continuous discharging.
[0023] 3. In the present invention, the high conversion rate of solar thermochemical cycle hydrogen production technology is adopted to solve the problem of sintering of conventional chemical cracking hydrogen production catalysts, which leads to difficulty in long-term production. Iron-nickel-iron oxides can be recycled, reducing production costs and having good social and economic benefits.
[0024] Other features and advantages of the present invention will be described in the following description, and partly become apparent from the description, or be understood by implementing the embodiments of the present invention. The purpose and other advantages of the present invention can be realized and obtained by the structures particularly pointed out in the written description, claims, and drawings. BRIEF DESCRIPTION OF THE DRAWINGS
[0025] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the embodiments are briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without creative work.
[0026] Figure 1 This is a schematic diagram of the overall process flow of a solar thermochemical cycle hydrogen production reactor proposed in the present invention.
[0027] Description of the accompanying drawings: 001, gas steam pipe; 002, catalyst lifting pipe; 003, regeneration inclined pipe; 004, to-be-regenerated inclined pipe; 101, first fluidized steam pipe; 102, water splitting reactor; 103, first cyclone separator; 104, first catalyst feed leg; 105, first quartz glass; 106, second cyclone separator; 107, second catalyst feed leg; 108, first outlet pipe; 201, second fluidized steam pipe; 202, catalyst regenerator; 203, third cyclone separator; 204, third catalyst feed leg; 205, second quartz glass; 206, second outlet pipe; 301, flow meter; 302, regulating valve. DETAILED DESCRIPTION
[0028] In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments. The components of the embodiments of the present invention generally described and shown in the drawings here can be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely represents selected embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.
[0029] It should be noted that similar reference numerals and letters represent similar items in the following drawings, so once an item is defined in one drawing, it does not need to be further defined and explained in the subsequent drawings. At the same time, in the description of the present invention, the terms "first", "second", etc. are only used to distinguish the description and cannot be understood as indicating or implying relative importance.
[0030] like Figure 1The present embodiment provides a solar thermochemical cycle hydrogen production reactor, comprising: a gas steam pipe 001, the gas steam pipe 001 is connected to the inlet of a catalyst lifting pipe 002, a water splitting reactor 102, the outlet of the catalyst lifting pipe 002 extends into the interior of the water splitting reactor 102, the stripping steam carries the catalyst through the gas steam pipe 001 and the catalyst lifting pipe 002 in sequence into the water splitting reactor 102, the catalyst in the water splitting reactor 102 undergoes an oxidation reaction under high temperature conditions to generate hydrogen, a catalyst regenerator 202, the catalyst regenerator 202 is connected to the water splitting reactor 102 through a to-be-regenerated inclined pipe 004 02 is connected, the catalyst after the reaction in the water splitting reactor 102 flows into the catalyst regenerator 202 through the waiting inclined pipe 004, and undergoes a reduction reaction under high temperature conditions to generate oxygen and regenerated catalyst, and the regenerated catalyst obtains activity under the action of oxygen, the catalyst regenerator 202 is connected with a regeneration inclined pipe 003, one end of the regeneration inclined pipe 003 is connected with the catalyst lifting pipe 002, the regenerated catalyst enters the water splitting reactor 102 through the regeneration inclined pipe 003 and the catalyst lifting pipe 002 in turn, and circulates to perform hydrogen production reaction, and fluidizing steam is introduced into the water splitting reactor 102 and the catalyst regenerator 202.
[0031] Among them, the stripping steam carrying the catalyst is first transported to the water splitting reactor 102 through the gas steam pipe 001, and the catalyst in the water splitting reactor 102 undergoes a chemical reaction under a high temperature state. The catalysts used in the water splitting reactor 102 are NiO and FeO, and NiO and FeO undergo an oxidation reaction under a high temperature state to produce hydrogen.
[0032] After reacting at high temperature, NiO and FeO will be converted into NiFe2O4, which will be input into the catalyst regenerator 202 through the inclined tube 004 to be regenerated, thereby forming a regenerated catalyst. The generated NiFe2O4 will undergo a reduction reaction in the catalyst regenerator 202 under high temperature, and the catalyst reduction will produce oxygen, NiO and FeO. NiO and FeO will regain their activity in an environment with oxygen, and will be transported to the water splitting reactor 102 through the catalyst lifting pipe 002 through the regeneration inclined tube 003, thereby cyclically carrying out the next round of hydrogen production reaction.
[0033] It should be noted that, during the chemical reaction of the water splitting reactor 102 and the catalyst regenerator 202, fluidized steam is continuously introduced from the bottom of the water splitting reactor 102 and the catalyst regenerator 202 to achieve a fluidized reaction of the catalyst and the reaction raw materials. The catalyst is in a fluidized state and a gas-solid two-phase flow state during the whole process, and the catalysts move relative to each other. At the same time, under the influence of the fluidized steam, the catalyst will not undergo high-temperature sintering, and the system can operate stably for a long period of time, with continuous feeding and continuous discharging. The conventional chemical cracking hydrogen production catalyst sintering, which leads to the problem of difficulty in long-term production, can be solved, and the iron-nickel-iron oxide can be recycled, which reduces the production cost and has good social and economic benefits.
[0034] The oxidation reaction is NiO+2FeO+H2O→NiFe2O4+H2
[0035] The reduction reaction is NiFe2O4→NiO+2FeO+1 / 2O2
[0036] In this embodiment, a first cyclone separator 103 is provided inside the water splitting reactor 102, and a second cyclone separator 106 is provided outside the water splitting reactor 102. The first cyclone separator 103 is connected to the outlet of the catalyst lifting pipe 002. The first cyclone separator 103 is used to classify the feed catalyst and the stripping steam, and the second cyclone separator 106 is used to separate the hydrogen, water and the carried catalyst at the outlet.
[0037] The stripping steam from outside the system carries the catalyst through the gas steam pipe 001 and the catalyst lifting pipe 002 in sequence, and is input into the first cyclone separator 103. The gas-solid mixture of the catalyst and steam is separated by the working principle of the first cyclone separator 103, and the steam enters the gas phase space. The second cyclone separator 106 is set to separate the products after the reaction in the water splitting reactor 102, and the regenerated catalyst is transported to the catalyst regenerator 202 through the inclined pipe to be regenerated 004 to undergo a reduction reaction in a high temperature environment.
[0038] In this embodiment, a third cyclone separator 206 is provided outside the catalyst regenerator 202, and the third cyclone separator 206 is used to separate the reaction products containing oxygen and the catalyst carried at the outlet. The third cyclone separator 206 is used to separate the products of the reaction in the catalyst regenerator 202, and the reaction products containing oxygen and the catalyst carried are transported through the regeneration inclined pipe 003, and are sequentially input into the water splitting reactor 102 through the catalyst lifting pipe 002 and the first cyclone separator 103 for the next cyclic hydrogen production reaction.
[0039] In this embodiment, air distribution plates are provided at the bottom of the water splitting reactor 102 and the catalyst regenerator 202, the first fluidized steam pipe 101 is connected to the bottom of the water splitting reactor 102, and the second fluidized steam pipe 201 is connected to the bottom of the catalyst regenerator 202, and the fluidized steam passes through the first fluidized steam pipe 101 or the second fluidized steam pipe 201 and then enters the water splitting reactor 102 or the catalyst regenerator 202 through the air distribution plate, and the air distribution plate is used for uniform distribution of the fluidized steam.
[0040] The first fluidizing steam pipe 101 and the second fluidizing steam pipe 201 are provided to input fluidizing steam into the water splitting reactor 102 or the catalyst regenerator 202, and the input fluidizing steam is used as the fluidizing medium of the water splitting reactor 102 or the catalyst regenerator 202. The air distribution plate is provided so that the fluidizing steam can evenly enter the interior of the reactor.
[0041] In this embodiment, the first cyclone separator 103 is connected to a first catalyst feed leg 104, the second cyclone separator 106 is connected to a second catalyst feed leg 107, the water splitting reactor 102 and the catalyst regenerator 202 both adopt fluidized bed reactors, the first catalyst feed leg 104 or the second catalyst feed leg 107 is used to input the catalyst separated by the first cyclone separator 103 or the second cyclone separator 106 into the bed layer of the fluidized bed of the water splitting reactor 102, the third cyclone separator 206 is connected to a third catalyst feed leg 204, and the third catalyst feed leg 204 is used to input the catalyst separated by the third cyclone separator 206 into the bed layer of the fluidized bed of the catalyst regenerator 202.
[0042] Among them, the water splitting reactor 102 and the catalyst regenerator 202 both adopt fluidized bed reactors. There are fluidized bed layers in the water splitting reactor 102 and the catalyst regenerator 202. The bed layers are divided into dense phase bed and dilute phase bed. The catalyst enters the catalyst fluidization space through the first catalyst feed leg 104, and the solid catalyst separated by the second cyclone separator 106 enters the reactor catalyst dense phase area through the second catalyst feed leg 107. The water splitting reactor 102 and the catalyst regenerator 202 adopt fluidized bed technology during the reaction, thereby avoiding the problem of high-temperature catalyst particle sintering.
[0043] In this embodiment, the top of the water splitting reactor 102 is provided with a first quartz glass 105, and the top of the catalyst regenerator 202 is provided with a second quartz glass 205, and the first quartz glass 105 and the second quartz glass 205 are used to allow external heat sources to enter the water splitting reactor 102 and the catalyst regenerator 202 through radiation to heat the catalyst and steam. By providing the first quartz glass 105 and the second quartz glass 205, light-transmitting holes are opened on the first quartz glass 105 and the second quartz glass 205, the reaction heat is provided by the dish-type concentrator to focus the solar energy, and the solar radiation heat is focused into the water splitting reactor 102 or the catalyst regenerator 202 through the opened light-transmitting holes, so that it is in a high-temperature environment, providing the required heat energy for the chemical reaction in the water splitting reactor 102 or the catalyst regenerator 202, and the high-temperature sunlight enters the reactor through radiation to heat the catalyst. When the water splitting reactor 102 or the catalyst regenerator 202 is in a high-temperature environment, the catalyst undergoes a chemical reaction to generate the desired product.
[0044] It should be noted that the temperature required for the oxidation reaction in the water splitting reactor 102 is 1000° C., and the temperature required for the reduction reaction in the catalyst regenerator 202 is 1400° C. Using high-temperature heat energy generated by focusing clean solar energy as a driving heat source can reduce production costs and has good social and economic benefits.
[0045] In this embodiment, the second cyclone separator 106 is connected to a first outlet pipe 108, and the first outlet pipe 108 is used to transport the gas product of the oxidation reaction to a heat exchanger for subsequent treatment. The third cyclone separator 203 is connected to a second outlet pipe 206, and the second outlet pipe 206 is used to transport the oxygen after the reaction to a heat exchanger for subsequent treatment. The first outlet pipe 108 and the second outlet pipe 206 are provided to facilitate subsequent processing of the product after the reaction of the water splitting reactor 102 or the catalyst regenerator 202, and the heat exchanger is installed at the outlet of the first outlet pipe 108 and the second outlet pipe 206 to perform subsequent heat exchange treatment on the product after the reaction.
[0046] In this embodiment, the inner walls of the water splitting reactor 102 and the catalyst regenerator 202 are made of high temperature resistant ceramic materials, and the outer walls of the water splitting reactor 102 and the catalyst regenerator 202 are provided with insulation plates, which are used to prevent heat loss. The high temperature resistant ceramic materials are used to provide the required environment for the water splitting reactor 102 and the catalyst regenerator 202 to perform high temperature reactions. It should be noted that the water splitting reactor 102 is at least made of a ceramic material that can withstand a high temperature of 1000°C, and the catalyst regenerator 202 is at least made of a ceramic material that can withstand a high temperature of 1400°C. High temperature resistant ceramic materials belong to existing known content, so the material of the water splitting reactor 102 and the catalyst regenerator 202 is not specifically introduced in this application. As long as the ceramic material that meets the above conditions can be used as the preparation material of the water splitting reactor 102 and the catalyst regenerator 202.
[0047] In this embodiment, the inlet of the fluidizing steam and the stripping steam are both provided with a flow meter 301 and a regulating valve 302, wherein the flow meter 301 is used to detect the flow value of the fluidizing steam or stripping steam inlet, and the regulating valve 302 is used to adjust the opening of the regulating valve 302 according to the flow required at the first fluidizing steam pipe 101 or the second fluidizing steam pipe 201 or the gas steam pipe 001. By setting a flow meter to detect the flow at the gas steam pipe 001, the first fluidizing steam pipe 101 and the second fluidizing steam pipe 201 in real time, and then adjusting the opening of the regulating valve 302, the flow at the gas steam pipe 001, the first fluidizing steam pipe 101 and the second fluidizing steam pipe 201 can be changed in real time according to the needs of the subsequent process flow.
[0048] In this embodiment, the water splitting reactor 102 is arranged at a height higher than the catalyst regenerator 202, and the catalyst regenerator 202 is higher than the inlet of the catalyst lifting pipe 002. The catalyst flows from the water splitting reactor 102 to the catalyst regenerator 202 by gravity, and the catalyst flows from the catalyst lifting pipe 002 to the water splitting reactor 102 by steam gas, and the system pressure is balanced. Through the high-low arrangement, a height difference in material level is generated, which drives the catalyst flow between the water splitting reactor 102 and the catalyst regenerator 202, and the reduced catalyst at a low material level is lifted into the water splitting reactor 102 through the catalyst lifting pipe 002. The above measures realize the circulation of the catalyst.
[0049] The working principle of the present invention is as follows: the stripping steam carries the catalyst and sequentially passes through the gas steam pipe 001 and the catalyst lifting pipe 002, is input into the first cyclone separator 103, and then enters the water splitting reactor 102. The working principle of the first cyclone separator 103 is used to separate the gas-solid mixture of the catalyst and the steam. The steam enters the gas phase space. The second cyclone separator 106 is set to separate the products after the reaction in the water splitting reactor 102. The regenerated catalyst is transported to the catalyst regenerator 202 through the waiting inclined pipe 004 to undergo a reduction reaction under a high temperature environment. The third cyclone separator 206 is used to separate the products of the reaction in the catalyst regenerator 202. The oxygen-containing reaction products and the carried catalyst are transported through the regeneration inclined pipe 003, and are sequentially input into the water splitting reactor 102 through the catalyst lifting pipe 002 and the first cyclone separator 103 to carry out the next cyclic hydrogen production reaction.
[0050] By setting the first fluidized steam pipe 101 and the second fluidized steam pipe 201, fluidized steam is input into the water splitting reactor 102 or the catalyst regenerator 202, and the fluidized steam is used as the fluidized medium of the water splitting reactor 102 or the catalyst regenerator 202. By setting the air distribution plate, the fluidized steam can be uniformly entered into the interior of the reactor. There are fluidized bed layers in the water splitting reactor 102 and the catalyst regenerator 202, and the bed layers are divided into dense bed and dilute bed. The catalyst enters the catalyst fluidization space through the first catalyst feed leg 104, and the solid catalyst separated by the second cyclone separator 106 enters the reactor catalyst dense phase area through the second catalyst feed leg 107. The water splitting reactor 102 and the catalyst regenerator 202 adopt fluidized bed technology during the reaction, which avoids the problem of high-temperature catalyst particle sintering. The reaction heat is provided by a dish-type concentrator that focuses solar energy. The solar radiation heat is focused into the water splitting reactor 102 or the catalyst regenerator 202 through the opened light-transmitting holes, thereby placing it in a high-temperature environment and providing the required thermal energy for the chemical reaction in the water splitting reactor 102 or the catalyst regenerator 202.
[0051] The stripping steam from outside the system carries the catalyst into the water splitting reactor 102, and the temperature of the water splitting reactor 102 reaches 1000°C by focusing the high temperature of solar energy. The fluidized steam carries the catalyst for chemical reaction, the catalyst is oxidized, and the water is decomposed into hydrogen, thereby realizing efficient hydrogen production from solar energy. In the catalyst regenerator 202, the temperature of the catalyst regenerator 202 reaches 1400°C by focusing the high temperature of solar energy, the catalyst is reduced to produce oxygen, the catalyst regains its activity, and the next round of hydrogen production reaction is circulated. The use of fluidized bed technology avoids the problem of sintering of high-temperature catalyst particles.
[0052] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.
[0053] The above is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art can easily think of changes or substitutions within the technical scope disclosed by the present invention, which should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.
Claims
1. A solar thermochemical cycle hydrogen production reactor, characterized in that: include: A gas steam pipe (001), wherein the gas steam pipe (001) is connected to the inlet of the catalyst riser (002); A water splitting reactor (102), wherein the outlet of the catalyst lifting pipe (002) extends into the interior of the water splitting reactor (102), and the stripping steam carries the catalyst through the gas steam pipe (001) and the catalyst lifting pipe (002) in sequence and enters the water splitting reactor (102), and the catalyst in the water splitting reactor (102) undergoes an oxidation reaction under high temperature conditions to generate hydrogen; A catalyst regenerator (202), wherein the catalyst regenerator (202) is connected to the water splitting reactor (102) through a waiting inclined tube (004), and the catalyst after the reaction in the water splitting reactor (102) flows into the catalyst regenerator (202) through the waiting inclined tube (004), and undergoes a reduction reaction under high temperature conditions to generate oxygen and regenerated catalyst, and the regenerated catalyst acquires activity under the action of oxygen; The catalyst regenerator (202) is connected to a regeneration inclined tube (003), one end of which is connected to a catalyst lifting tube (002). The regenerated catalyst passes through the regeneration inclined tube (003) and the catalyst lifting tube (002) in sequence and enters the water splitting reactor (102) to circulate and perform a hydrogen production reaction. Fluidizing steam is introduced into the water splitting reactor (102) and the catalyst regenerator (202).
2. A solar thermochemical cycle hydrogen production reactor according to claim 1, characterized in that: A first cyclone separator (103) is provided inside the water splitting reactor (102), and a second cyclone separator (106) is provided outside the water splitting reactor (102). The first cyclone separator (103) is connected to the outlet of the catalyst lifting pipe (002). The first cyclone separator (103) is used to classify the feed catalyst and the stripping steam, and the second cyclone separator (106) is used to separate the hydrogen, water and the carried catalyst at the outlet.
3. A solar thermochemical cycle hydrogen production reactor according to claim 2, characterized in that: A third cyclone separator (206) is disposed outside the catalyst regenerator (202), and the third cyclone separator (206) is used to separate the oxygen-containing reaction product at the outlet and the carried catalyst.
4. A solar thermochemical cycle hydrogen production reactor according to claim 3, characterized in that: The bottom of the water splitting reactor (102) and the catalyst regenerator (202) are both provided with an air distribution plate. The first fluidized steam pipe (101) is connected to the bottom of the water splitting reactor (102), and the second fluidized steam pipe (201) is connected to the bottom of the catalyst regenerator (202). The fluidized steam passes through the first fluidized steam pipe (101) or the second fluidized steam pipe (201) and then enters the water splitting reactor (102) or the catalyst regenerator (202) through the air distribution plate. The air distribution plate is used for uniform distribution of the fluidized steam.
5. A solar thermochemical cycle hydrogen production reactor according to claim 4, characterized in that: The first cyclone separator (103) is connected to a first catalyst feed leg (104), the second cyclone separator (106) is connected to a second catalyst feed leg (107), the water splitting reactor (102) and the catalyst regenerator (202) both adopt fluidized bed reactors, the first catalyst feed leg (104) or the second catalyst feed leg (107) is used to input the catalyst separated by the first cyclone separator (103) or the second cyclone separator (106) into the bed layer of the fluidized bed of the water splitting reactor (102), the third cyclone separator (206) is connected to a third catalyst feed leg (204), the third catalyst feed leg (204) is used to input the catalyst separated by the third cyclone separator (206) into the bed layer of the fluidized bed of the catalyst regenerator (202).
6. A solar thermochemical cycle hydrogen production reactor according to claim 1, characterized in that: A first quartz glass (105) is provided on the top of the water splitting reactor (102), and a second quartz glass (205) is provided on the top of the catalyst regenerator (202). The first quartz glass (105) and the second quartz glass (205) are used to allow an external heat source to enter the water splitting reactor (102) and the catalyst regenerator (202) through radiation to heat the catalyst and steam.
7. A solar thermochemical cycle hydrogen production reactor according to claim 3, characterized in that: The second cyclone separator (106) is connected to a first outlet pipe (108), and the first outlet pipe (108) is used to transport the gas product of the oxidation reaction to a heat exchanger for subsequent treatment. The third cyclone separator (203) is connected to a second outlet pipe (206), and the second outlet pipe (206) is used to transport the oxygen after the reaction to a heat exchanger for subsequent treatment.
8. The solar thermochemical cycle hydrogen production reactor according to claim 1, characterized in that: The inner walls of the water splitting reactor (102) and the catalyst regenerator (202) are both made of high-temperature resistant ceramic materials, and the outer walls of the water splitting reactor (102) and the catalyst regenerator (202) are provided with insulation plates, which are used to prevent heat loss.
9. A solar thermochemical cycle hydrogen production reactor according to claim 4, characterized in that: The inlets of the fluidizing steam and the stripping steam are both provided with a flow meter (301) and a regulating valve (302), wherein the flow meter (301) is used to detect the flow value of the fluidizing steam or stripping steam inlet, and the regulating valve (302) is used to adjust the opening of the regulating valve (302) according to the flow required at the first fluidizing steam pipe (101) or the second fluidizing steam pipe (201) or the gas steam pipe (001).
10. A solar thermochemical cycle hydrogen production reactor according to claim 4, characterized in that: The water splitting reactor (102) is arranged at a height higher than the catalyst regenerator (202), and the catalyst regenerator (202) is higher than the inlet of the catalyst riser (002). The catalyst flows from the water splitting reactor (102) to the catalyst regenerator (202) by gravity flow, and the catalyst flows from the catalyst riser (002) to the water splitting reactor (102) by steam gas, and the system pressure is balanced.