System for producing hydrogen through solar photo-thermal catalytic fluidization reaction

Abstract

The utility model discloses a system for producing hydrogen through solar photo-thermal catalytic fluidization reaction. The system comprises a reduction reactor, a first waste heat recovery and heat exchange mechanism, a first pipeline, a first gas supply mechanism, an oxidation reactor, a second gas supply mechanism, a second pipeline, a third pipeline and a second waste heat recovery and heat exchange mechanism. A catalyst is arranged in the reduction reactor, and the reduction reactor is used for reducing the catalyst to obtain the reduced catalyst and a first mixed gas. The first waste heat recovery and heat exchange mechanism is arranged outside the reduction reactor, and the first waste heat recovery and heat exchange mechanism is used for receiving the first mixed gas and generating oxygen. And the second waste heat recovery heat exchange mechanism is used for receiving the second mixed gas and generating hydrogen. The technical scheme provided by the embodiment of the utility model is low-carbon and environment-friendly, and can produce hydrogen on an industrial economic scale.

Description

Technical Field

[0001] The utility model relates to the technical field of hydrogen production, in particular to a system for producing hydrogen through solar photothermal catalytic fluidized reaction. Background Art

[0002] my country has an annual hydrogen production capacity of 40 million tons and an annual output of 33 million tons. It is the world's largest hydrogen producer, mainly gray hydrogen for industrial production and processing. Hydrogen-using enterprises are mainly in the fields of oil refining, chemical industry, fertilizer, steelmaking, etc., and a small amount is used as industrial fuel. The raw materials for hydrogen production are mainly fossil sources, including natural gas, coal, petroleum refining dry gas, olefin cracking, etc.

[0003] By the end of 2023, my country has put into production 850,000 tons / year of green hydrogen production capacity, accounting for only about 2% of the total hydrogen production capacity. The production technology is mainly alkaline electrolyzer, and a small number of devices use proton exchange membrane (PEM) technology. All industries and regions need to build renewable green hydrogen production capacity (mainly relying on alkaline electrolyzer technology) of at least 100GW by 2030, equivalent to a green hydrogen production capacity of about 5 million tons / year.

[0004] However, the existing solar photovoltaic water electrolysis hydrogen production energy utilization efficiency is less than 20%, which does not have obvious efficiency advantages and economic benefits.

[0005] The information disclosed in this background technology section is only intended to increase the understanding of the overall background of the present invention, and should not be regarded as acknowledging or suggesting in any form that the information constitutes the prior art already known to a person skilled in the art. Utility Model Content

[0006] The purpose of the utility model is to provide a system for producing hydrogen by solar thermal catalytic fluidized reaction, which is low-carbon and environmentally friendly, and can industrially produce hydrogen for producing sustainable renewable fuel or chemical synthesis raw materials, and improves energy utilization efficiency.

[0007] To achieve the above-mentioned purpose, the utility model provides a system for producing hydrogen by solar thermal catalytic fluidized reaction, including: a reduction reactor, a first waste heat recovery and heat exchange mechanism, a first pipeline, a first gas supply mechanism, an oxidation reactor, a second gas supply mechanism, a second pipeline, a third pipeline and a second waste heat recovery and heat exchange mechanism. The reduction reactor is equipped with a catalyst, and the reduction reactor is used to reduce the catalyst to obtain a reduced catalyst and a first mixed gas. The first waste heat recovery and heat exchange mechanism is arranged outside the reduction reactor, and the first waste heat recovery and heat exchange mechanism is used to receive the first mixed gas and generate oxygen. One end of the first pipeline is connected to the bottom of the reduction reactor. The first gas supply mechanism is connected to the other end of the first pipeline, and the first gas supply mechanism is used to provide a first gas to the reduction reactor, so as to fluidize the catalyst and serve as a reactant. The oxidation reactor is used to oxidize the reduced catalyst to obtain the catalyst and a second mixed gas. The second gas supply mechanism is connected to the oxidation reactor through a lifting pipeline, and the second gas supply mechanism is used to provide a second gas to the oxidation reactor. One end of the second pipeline is connected to the reduction reactor, and the other end of the second pipeline is connected to the lifting pipeline. One end of the third pipeline is connected to the oxidation reactor, and the other end of the third pipeline is connected to the reduction reactor. And the second waste heat recovery heat exchange mechanism is arranged outside the oxidation reactor, and the second waste heat recovery heat exchange mechanism is used to receive the second mixed gas and generate hydrogen.

[0008] In one embodiment of the utility model, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes: a third gas supply mechanism, which is connected to the bottom of the oxidation reactor through a fourth pipeline, and is used to provide a third gas to the oxidation reactor for fluidization and as a reactant.

[0009] In one embodiment of the utility model, the solar photothermal catalytic fluidized reaction system for producing hydrogen further includes: a high-temperature focusing mechanism and a light-transmitting mirror. The high-temperature focusing mechanism is used to provide solar photothermal energy. The light-transmitting mirror is arranged on the top of the reduction reactor, and the light-transmitting mirror is used to receive the solar photothermal energy provided by the high-temperature focusing mechanism, and introduce the solar photothermal energy into the reduction reactor, thereby heating the reduction reactor.

[0010] In one embodiment of the utility model, the solar thermal catalytic fluidized reaction system for producing hydrogen further includes: a high-temperature heat storage tank and a seventh pipeline. The high-temperature heat storage tank is connected to the reduction reactor through a fifth pipeline and a sixth pipeline respectively; and one end of the seventh pipeline is connected to the bottom of the high-temperature heat storage tank, and the other end of the seventh pipeline is connected to the first pipeline.

[0011] In one embodiment of the utility model, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a control mechanism, a first flow control valve, a second flow control valve, a third flow control valve, a fourth flow control valve, a first electrically controlled valve, a second electrically controlled valve and a third electrically controlled valve. The first flow control valve is arranged on the first pipeline, and the first flow control valve is electrically connected to the control mechanism. The second flow control valve is arranged on the second pipeline, and the second flow control valve is electrically connected to the control mechanism. The third flow control valve is arranged on the third pipeline, and the third flow control valve is electrically connected to the control mechanism. The fourth flow control valve is arranged on the fourth pipeline, and the fourth flow control valve is electrically connected to the control mechanism. The first electrically controlled valve is arranged on the fifth pipeline, and the first electrically controlled valve is electrically connected to the control mechanism. The second electrically controlled valve is arranged on the sixth pipeline, and the second electrically controlled valve is electrically connected to the control mechanism. And the third electrically controlled valve is arranged on the seventh pipeline, and the third electrically controlled valve is electrically connected to the control mechanism. Among them, the control mechanism can control the opening and closing of the first flow control valve, the second flow control valve, the third flow control valve, the fourth flow control valve, the first electrically-controlled valve, the second electrically-controlled valve and the third electrically-controlled valve respectively.

[0012] In one embodiment of the utility model, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes: a catalyst heat collector, an eighth pipeline, a ninth pipeline, a fourth electrically controlled valve and a fifth electrically controlled valve. The catalyst heat collector is arranged on the outside of the oxidation reactor. One end of the eighth pipeline is connected to the bottom of the catalyst heat collector, and the other end of the eighth pipeline is connected to the oxidation reactor. One end of the ninth pipeline is connected to the upper part of the catalyst heat collector, and the other end of the ninth pipeline is connected to the oxidation reactor. The fourth electrically controlled valve is arranged on the eighth pipeline, and the fourth electrically controlled valve is electrically connected to the control mechanism. And the fifth electrically controlled valve is arranged on the ninth pipeline, and the fifth electrically controlled valve is electrically connected to the control mechanism. Wherein, the control mechanism can control the opening and closing of the fourth electrically controlled valve and the fifth electrically controlled valve respectively.

[0013] In one embodiment of the utility model, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes: a first gas-solid separator and a second gas-solid separator. The first gas-solid separator is arranged on the outside of the reduction reactor, and the first gas-solid separator is connected to the reduction reactor through a first recovery pipeline and a second recovery pipeline respectively, and the first gas-solid separator is also connected to the first waste heat recovery heat exchange mechanism through a third recovery pipeline. And the second gas-solid separator is arranged on the outside of the oxidation reactor, and the second gas-solid separator is connected to the oxidation reactor through a fourth recovery pipeline and a fifth recovery pipeline, and the second gas-solid separator is also connected to the second waste heat recovery heat exchange mechanism through a sixth recovery pipeline.

[0014] In one embodiment of the utility model, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a first stripping tower and a second stripping tower. The first end of the first stripping tower is connected to the reduction reactor through the second pipeline, the second end of the first stripping tower is connected to the oxidation reactor through the second pipeline and the lifting pipeline, and the third end of the first stripping tower is connected to the reduction reactor through the tenth pipeline. And the first end of the second stripping tower is connected to the reduction reactor through the third pipeline, the second end of the second stripping tower is connected to the oxidation reactor through the third pipeline, and the third end of the second stripping tower is connected to the oxidation reactor through the eleventh pipeline.

[0015] In one embodiment of the utility model, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes: a fourth gas supply mechanism, a twelfth pipeline, a thirteenth pipeline and a fifth flow control valve. One end of the twelfth pipeline is connected to the fourth gas supply mechanism, and the other end of the twelfth pipeline is connected to the bottom of the second stripping tower. One end of the thirteenth pipeline is connected to the twelfth pipeline, and the other end of the thirteenth pipeline is connected to the bottom of the first stripping tower. And the fifth flow control valve is arranged on the twelfth pipeline, and the fifth flow control valve is electrically connected to the control mechanism. Among them, the fourth gas supply mechanism is used to provide the fourth gas to the second stripping tower and the first stripping tower through the twelfth pipeline and the thirteenth pipeline respectively.

[0016] In one embodiment of the utility model, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes a heat exchange mechanism, a first end of the heat exchange mechanism is connected to the first stripping tower through the second pipeline, a second end of the heat exchange mechanism is connected to the lifting pipeline through the second pipeline, a third end of the heat exchange mechanism is connected to the reduction reactor through the third pipeline, and a fourth end of the heat exchange mechanism is connected to the second stripping tower through the third pipeline.

[0017] Compared with the prior art, the solar photothermal catalytic fluidized reaction system for producing hydrogen according to the utility model is low-carbon and environmentally friendly, and can industrially produce hydrogen for producing sustainable renewable fuels or chemical synthesis raw materials, and improves energy utilization efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 This is a schematic structural diagram of a system for producing hydrogen by solar thermal catalytic fluidized reaction according to one embodiment of the utility model;

[0019] Figure 2 It is a structural schematic diagram of a first waste heat recovery and heat exchange mechanism according to an embodiment of the utility model;

[0020] Figure 3 is another structural schematic diagram of the first waste heat recovery and heat exchange mechanism according to one embodiment of the utility model;

[0021] Figure 4 It is a structural schematic diagram of a second waste heat recovery and heat exchange mechanism according to an embodiment of the utility model;

[0022] Figure 5 It is a structural schematic diagram of a heat storage type heat exchange mechanism according to a specific implementation mode of the utility model;

[0023] Figure 6 It is another structural schematic diagram of a system for producing hydrogen through solar thermal catalytic fluidized reaction according to one embodiment of the utility model.

[0024] Description of main reference numerals:

[0025] 1-reduction reactor, 2-first waste heat recovery heat exchange mechanism, 3-first pipeline, 4-first gas supply mechanism, 5-sixth flow control valve, 6-oxidation reactor, 7-second waste heat recovery heat exchange mechanism, 8-second gas supply mechanism, 9-lifting pipeline, 10-second pipeline, 11-third pipeline, 12-third gas supply mechanism, 13-fourth pipeline, 14-high temperature focusing mechanism, 15-light-transmitting mirror, 16-high temperature heat storage tank, 17-fifth pipeline, 18-sixth pipeline, 19-seventh pipeline, 20-first flow control valve, 21-second flow control valve, 22-third flow control valve, 23-fourth flow control valve, 24-first electric control valve, 25-second electric control valve, 26-third electric control valve, 27-catalyst heat collector, 28-eighth pipeline, 29-ninth pipeline, 30-fourth electric control Valve, 31-fifth electrically controlled valve, 32-first gas-solid separator, 33-first recovery pipeline, 34-second recovery pipeline, 35-third recovery pipeline, 36-second gas-solid separator, 37-fourth recovery pipeline, 38-fifth recovery pipeline, 39-sixth recovery pipeline, 40-first stripping tower, 41-tenth pipeline, 42-second stripping tower, 43-eleventh pipeline, 44-fourth gas supply mechanism, 45-twelfth pipeline, 46-thirteenth pipeline, 47-fifth flow control valve, 48-heat exchange mechanism, 49-first heat exchanger, 50-first cooler, 51-PSA unit, 52-second heat exchanger, 53-second cooler, 54-first deaerator, 55-steam generator, 56-second deaerator, 57-four-way valve, 58-heat storage heat exchanger, 59-fourteenth pipeline. DETAILED DESCRIPTION

[0026] The following is a further detailed description of the embodiments of the utility model in conjunction with the accompanying drawings and embodiments. It is to be understood that the specific embodiments described herein are only used to explain the embodiments of the utility model, rather than to limit the embodiments of the utility model. It should also be noted that, for ease of description, only parts related to the embodiments of the utility model are shown in the accompanying drawings, rather than all structures.

[0027] For ease of understanding, the main implementation concepts of each embodiment of the present utility model are first briefly described.

[0028] The embodiment of the utility model utilizes solar heat to heat a metal oxide catalyst, and decomposes water through a two-step reduction and oxidation cycle reaction to generate hydrogen and oxygen for producing sustainable renewable fuels or chemical synthesis raw materials. Since the embodiment of the utility model is based on renewable energy and raw materials, it is not limited by the supply of raw materials, and industrial production can meet market demand.

[0029] The two-step cycle reaction of thermochemical reduction and oxidation based on metal oxides as catalysts can efficiently utilize the heat provided by solar energy to produce hydrogen, and the metal oxide catalysts selected in the embodiments of the present invention include but are not limited to cerium oxide, iron oxide, nickel oxide, manganese oxide and oxides of two or more metals.

[0030] Figure 1 Schematic diagram of a system for producing hydrogen by solar thermal catalytic fluidized reaction according to an embodiment of the present invention. Figure 1 As shown, the utility model provides a system for producing hydrogen by solar thermal catalytic fluidized reaction, comprising: a reduction reactor 1, a first waste heat recovery heat exchange mechanism 2, a first pipeline 3, a first gas supply mechanism 4, an oxidation reactor 6, a second gas supply mechanism 8, a second pipeline 10, a third pipeline 11, a second waste heat recovery heat exchange mechanism 7 and a third gas supply mechanism 12. The reduction reactor 1 has a catalyst built therein, and the reduction reactor 1 is used to reduce the catalyst to obtain the reduced catalyst and the first mixed gas.

[0031] Specifically, the catalyst is selected from metal oxides (M x O y ), the metal oxides include, for example, iron, nickel, copper, magnesium, manganese, zinc, cobalt, cerium, etc., alumina Al2O3 is used as a carrier, the average particle diameter is about 100 μm to 200 μm, the micropore diameter is 3 nm to 6 nm, and the specific surface area is 200 m 2 / g~250m 2 / g.

[0032] The first waste heat recovery and heat exchange mechanism 2 is disposed outside the reduction reactor 1, and the first waste heat recovery and heat exchange mechanism 2 is used to receive the first mixed gas (the first mixed gas at this time includes oxygen and fluidizing gas) and generate oxygen.

[0033] Specifically, if the first gas uses helium as the fluidizing gas, Figure 2 As shown, the first waste heat recovery heat exchange mechanism 2 includes a first heat exchanger 49, a first cooler 50 and a PSA unit 51 (PSA, Pressure Swing Adsorption) connected in sequence; when the first mixed gas enters the first heat exchanger 49, the mixed gas exchanges heat with the fluidizing gas, and the heated fluidizing gas is transported back to the reduction reactor 1; the cooled mixed gas continues to enter the first cooler 50 for cooling, and then enters the PSA unit 51 for separating oxygen and fluidizing gas, and the separated fluidizing gas is returned to the first heat exchanger 49.

[0034] Specifically, if steam is used as the fluidizing gas, Figure 3As shown, the first waste heat recovery heat exchange mechanism 2 includes a second heat exchanger 52, a second cooler 53 and a first deoxygenation tank 54 which are connected in sequence; when the first mixed gas enters the second heat exchanger 52, the mixed gas heats the deoxygenated water and is then transported back to the reduction reactor 1; the cooled mixed gas continues to enter the second cooler 53 for cooling, and then enters the first deoxygenation tank 54 to separate condensed water and oxygen; the first deoxygenation tank 54 is used to remove oxygen from the condensed water and desalted water, and transport the water with oxygen removed (deoxygenated water) to the second heat exchanger 52.

[0035] One end of the first pipeline 3 is connected to the bottom of the reduction reactor 1. The first gas supply mechanism 4 is connected to the other end of the first pipeline 3, and the first gas supply mechanism 4 is used to provide a first gas to the reduction reactor 1, so as to fluidize the catalyst and serve as a reactant.

[0036] Specifically, a first feed gas distributor is provided at the bottom of the reduction reactor 1, the input end of the first feed gas distributor is connected to the one end of the first pipeline 3, and the other end of the first feed gas distributor extends into the catalyst bed at the bottom of the reduction reactor 1, and the first feed gas distributor is used to evenly distribute the first gas to the interior of the reduction reactor 1, so that the first gas fluidizes the catalyst, and then the fluidized catalyst serves as a reactant in the reduction reactor 1; wherein, the first feed gas distributor may be, for example, a tubular distributor or a plate distributor; wherein, the first gas may be, for example, helium, steam, or a mixture of several gases; wherein, the first feed gas distributor is an important internal component of the reduction reactor 1, which ensures uniform distribution of gas and stability of the bed.

[0037] The oxidation reactor 6 is used to oxidize the reduced catalyst to obtain the catalyst and the second mixed gas (the second mixed gas at this time includes hydrogen and water vapor). The second waste heat recovery heat exchange mechanism 7 is arranged outside the oxidation reactor 6, and the second waste heat recovery heat exchange mechanism 7 is used to receive the second mixed gas and generate hydrogen.

[0038] Specifically, Figure 4 As shown, the second waste heat recovery and heat exchange mechanism 7 includes a steam generator 55 and a second deaerator 56 connected in sequence. When the second mixed gas enters the steam generator 55, the mixed gas evaporates the deoxygenated water to generate high-pressure steam, and the high-pressure steam can be recovered for use in public works; the cooled hydrogen and condensed water enter the second deaerator 56 to separate the condensed water and hydrogen; the second deaerator 56 deoxygenates the condensed water and desalted water, and transports the water with oxygen removed (deoxygenated water) to the steam generator 55.

[0039] The second gas supply mechanism 8 is connected to the oxidation reactor 6 through the lifting pipeline 9, and the second gas supply mechanism 8 is used to provide the second gas to the oxidation reactor 6. One end of the second pipeline 10 is connected to the reduction reactor 1, and the other end of the second pipeline 10 is connected to the lifting pipeline 9. One end of the third pipeline 11 is connected to the oxidation reactor 6, and the other end of the third pipeline 11 is connected to the reduction reactor 1. Among them, the second gas supply mechanism 8 is connected to the lifting pipeline 9 through the fourteenth pipeline 59, and the six flow control valve 5 is provided on the fourteenth pipeline 59, and the sixth flow control valve 5 is electrically connected to the control mechanism.

[0040] Specifically, the second gas may be, for example, superheated steam (from a 0.5 MPa steam network); the second gas pushes the reduction catalyst in the riser into the oxidation reactor 6, and reacts with the catalyst in the oxidation reactor 6 to produce hydrogen.

[0041] The chemical reaction balance is:

[0042] M x O y-δ +δH2O→M x O y +δH2

[0043] The reduction reactor 1 and the oxidation reactor 6 are connected via the second pipeline 10, the lifting pipeline 9 and the third pipeline 11; wherein Figure 1 As shown, the lifting pipeline 9 is arranged outside the oxidation reactor 6. In another embodiment, as shown in Figure 6 As shown, the lifting pipeline 9 can also be arranged inside the oxidation reactor 6; wherein, when the lifting pipeline 9 is arranged inside the oxidation reactor 6, the material of the lifting pipeline 9 adopts a composite ceramic tube with good thermal conductivity. Its thermal conductivity is in the range of 200-3000W / mK, which increases the heat exchange effect of the catalyst; wherein, Figure 1 and Figure 6 The difference in the structural arrangement of is only the layout position of the lifting pipeline 9, and the others are the same, so Figure 6 The reference numerals are simplified.

[0044] The third gas supply mechanism 12 is connected to the bottom of the oxidation reactor 6 through a fourth pipeline 13, and the third gas supply mechanism 12 is used to provide a third gas to the oxidation reactor 6 for fluidization and as a reactant.

[0045] Specifically, a second feed gas distributor is provided at the bottom of the oxidation reactor 6, the third gas supply mechanism 12 is connected to the input end of the second feed gas distributor through the fourth pipeline 13, and the other end of the second feed gas distributor extends into the catalyst bed at the bottom of the oxidation reactor 6, and the second feed gas distributor is used to evenly distribute the third gas to the interior of the oxidation reactor 6; wherein, the second feed gas distributor may be, for example, a tubular distributor or a plate distributor; wherein, the tubular distributor may include a dendritic and annular shape; wherein, the second feed gas distributor is an important internal component of the oxidation reactor 6, which ensures uniform distribution of gas and stability of the bed.

[0046] In this embodiment, the solar photothermal catalytic fluidized reaction system for producing hydrogen further includes: a high-temperature focusing mechanism 14 and a light-transmitting mirror 15. The high-temperature focusing mechanism 14 is used to provide solar photothermal energy. The light-transmitting mirror 15 is disposed on the top of the reduction reactor 1, and the light-transmitting mirror 15 is used to receive the solar photothermal energy provided by the high-temperature focusing mechanism 14, and introduce the solar photothermal energy into the reduction reactor 1, thereby heating the reduction reactor 1.

[0047] Specifically, the light-transmitting mirror 15 is made of high-temperature resistant quartz glass, and flexible carbon fibers are arranged inside the glass, which can significantly enhance the strength of the quartz glass without affecting the light transmittance of the glass. The diameter of the light-transmitting mirror 15 is 1 / 4-1 / 2 of the diameter of the reduction reactor 1, and the preferred value is 1 / 3, which can effectively reduce the high-temperature radiation inside the reduction reactor 1.

[0048] In this embodiment, the solar thermal catalytic fluidized reaction system for producing hydrogen further includes: a high-temperature heat storage tank 16 and a seventh pipeline 19. The high-temperature heat storage tank 16 is connected to the reduction reactor 1 through a fifth pipeline 17 and a sixth pipeline 18 respectively; and one end of the seventh pipeline 19 is connected to the bottom of the high-temperature heat storage tank 16, and the other end of the seventh pipeline 19 is connected to the first pipeline 3.

[0049] Specifically, the high temperature heat storage tank 16 is mainly used to store hot catalysts, so as to ensure that the overall system can work continuously at night or when there is no sunlight; the working process at night or when there is no sunlight is as follows:

[0050] 1. Low operating load 30%, minimum fluidizing load 30%;

[0051] 2. Regulating the second flow control valve 21 on the second pipeline 10 between the reduction reactor 1 and the lifting pipeline 9 of the oxidation reactor 6, controlling the opening of the second flow control valve 21 according to the production requirement to reduce the catalyst circulation amount, and reducing the second gas (for example, superheated steam, provided by the second gas supply mechanism 8) injected into the bottom of the lifting pipeline 9, and continuing to feed the fluidizing steam into the oxidation reactor 6;

[0052] 3. Adjust the opening of the connecting valve (the first electrically controlled valve 24 and the second electrically controlled valve 25) between the reduction reactor 1 and the high-temperature heat storage tank 16. By reasonably arranging the height of the reduction reactor 1 and the high-temperature heat storage tank 16 (the reduction reactor 1 is higher than the high-temperature heat storage tank 16), the catalyst is fluidized by gravity, and the catalyst (1400° C. to 1500° C.) stored in the high-temperature heat storage tank supplements the heat required for the reaction of the system.

[0053] 4. Lower the bottom of the reduction reactor 1 to the minimum fluidization flow rate according to production requirements;

[0054] 5. Turn off the catalyst heat collector 27 outside the oxidation reactor 6;

[0055] 6. Keep the temperature of the oxidation reactor 6 and the reduction reactor 1 consistent (900-1000° C.);

[0056] 7. A certain amount of methane and oxygen may also be introduced to allow methane to burn and release heat inside the reduction reactor 1 to supplement the heat required for the reaction;

[0057] 8. Under low conversion rate conditions, it can run continuously at night.

[0058] Specifically, when the device is started, the connecting valves (the first electrically controlled valve 24 and the second electrically controlled valve 25) between the reduction reactor 1 and the high-temperature heat storage tank 16 are opened, and then fluidizing gas (provided by the first gas supply mechanism 4) is injected into the bottom of the high-temperature heat storage tank 16 to allow the catalyst to flow between the reduction reactor 1 and the high-temperature heat storage tank 16.

[0059] The high-temperature focusing mechanism 14 and the light-transmitting mirror 15 introduce the solar energy heat into the reduction reactor 1, thereby heating the reduction reactor 1. When the temperature of the catalyst in the reduction reactor 1 and the high-temperature heat storage tank 16 rises to 1500°C, the connecting valves (the first electrically controlled valve 24 and the second electrically controlled valve 25) between the reduction reactor 1 and the high-temperature heat storage tank 16 are closed, and the high-temperature heat storage tank 16 stores the catalyst after high-temperature reduction for standby use.

[0060] The thermometer in the reduction reactor 1 is interlocked with the control mechanism of the first electrically controlled valve 24 and the second electrically controlled valve 25. When the temperature in the reduction reactor 1 is lower than 1400°C, the first electrically controlled valve 24 and the second electrically controlled valve 25 will automatically open to provide high-temperature catalyst for the reduction reactor 1.

[0061] In this embodiment, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a control mechanism, a first flow control valve 20, a second flow control valve 21, a third flow control valve 22, a fourth flow control valve 23, a first electrically controlled valve 24, a second electrically controlled valve 25, and a third electrically controlled valve 26. The first flow control valve 20 is arranged on the first pipeline 3, and the first flow control valve 20 is electrically connected to the control mechanism. The second flow control valve 21 is arranged on the second pipeline 10, and the second flow control valve 21 is electrically connected to the control mechanism. The third flow control valve 22 is arranged on the third pipeline 11, and the third flow control valve 22 is electrically connected to the control mechanism. The fourth flow control valve 23 is arranged on the fourth pipeline 13, and the fourth flow control valve 23 is electrically connected to the control mechanism. The first electrically controlled valve 24 is arranged on the fifth pipeline 17, and the first electrically controlled valve 24 is electrically connected to the control mechanism. The second electrically controlled valve 25 is disposed on the sixth pipeline 18, and the second electrically controlled valve 25 is electrically connected to the control mechanism. The third electrically controlled valve 26 is disposed on the seventh pipeline 19, and the third electrically controlled valve 26 is electrically connected to the control mechanism. The control mechanism can respectively control the opening and closing of the first flow control valve 20, the second flow control valve 21, the third flow control valve 22, the fourth flow control valve 23, the first electrically controlled valve 24, the second electrically controlled valve 25, and the third electrically controlled valve 26.

[0062] Specifically, the control mechanism may include a reactor control system and a safety protection system, wherein the reactor safety protection system refers to a protection system for preventing gas backflow and gas isolation between the oxidation reactor 6 and the reduction reactor 1. The safety protection logic sets the differential pressure control protection between the reduction reactor 1 and the oxidation reactor 6, and when the differential pressure is low, the opening of the second flow control valve 21 or the third flow control valve 22 is locked. When the differential pressure between the two reactors is low, the flow control valves on the connecting pipelines of the two reactors are closed and the feeding is stopped; for example, the differential pressure between the two reactors is measured by a differential pressure gauge composed of pressure measuring points respectively arranged at the tops of the two reactors. The normal setting value of the differential pressure between the two reactors is 30kPa, the high alarm value of the differential pressure is 80kPa, the low alarm value is 25kPa, the high-high interlock value of the differential pressure is 100kPa, and the low-low interlock value of the differential pressure is 15kPa. When the pressure drop of the slide valve is lower than 15kPa, the opening of the slide valve is "soft locked". When the differential pressure between the two vessels is higher than 100 kPa or lower than 15 kPa, the differential pressure interlock is triggered, the oxidation catalyst slide valve and the reduction catalyst slide valve are closed, and the feed to the two reactors is stopped, and the two reactors are operated in a "stifled" mode.

[0063] Specifically, the reactor control system includes temperature control and pressure control of the two reactors (i.e., each pipeline can be provided with a temperature sensor and a pressure sensor, and each temperature sensor and each pressure sensor are electrically connected to the control mechanism). The temperature of the oxidation reactor 6 is controlled by the opening of the second flow control valve 21, and is assisted by the external heat exchanger when necessary. For example: the heat of the oxidation reactor 6 comes from the catalyst of the reduction reactor 1, and the set temperature of the oxidation reactor 6 is 900°C. When the temperature of the oxidation reactor 6 is lower than 900°C, the opening of the catalyst slide valve of the external heat exchanger is firstly closed to reduce the heat intake. When the heat intake load of the heat exchanger is lower than 30%, the external heat exchanger has no regulating capacity. At this time, it is necessary to open the opening of the reduction catalyst slide valve to control the temperature of the oxidation reactor 6. If the temperature is higher than the set value, the reduction catalyst slide valve is closed. The temperature of the reduction reactor 1 is controlled by the solar energy intake entering the top of the reaction; when it is nighttime or there is no solar energy input, the catalyst in the high-temperature heat storage tank 16 is used to supplement the heat or methane is burned to maintain the reaction temperature. The pressure of the oxidation reactor 6 is controlled by the gas line regulating valve at its top. The pressure of reduction reactor 1 is controlled by the gas line regulating valve at the top of the reactor. At the same time, it is automatically switched to the lower selected value according to the differential pressure of the two reactors. For example, during normal production, the pressure of the two reactors is controlled separately to keep the differential pressure of the two reactors within the set reasonable range (such as 40kPa). If the differential pressure of the two reactors exceeds a certain range, the differential pressure controller of the two reactors will replace the pressure controller to control the differential pressure of the two reactors, in order to make the fluidization of the two reactors smooth, and finally prevent the media of the two reactors from backflowing and mutual channeling, causing safety accidents.

[0064] In this embodiment, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a catalyst heat collector 27, an eighth pipeline 28, a ninth pipeline 29, a fourth electrically controlled valve 30 and a fifth electrically controlled valve 31. The catalyst heat collector 27 is arranged on the outside of the oxidation reactor 6. One end of the eighth pipeline 28 is connected to the bottom of the catalyst heat collector 27, and the other end of the eighth pipeline 28 is connected to the oxidation reactor 6. One end of the ninth pipeline 29 is connected to the upper part of the catalyst heat collector 27, and the other end of the ninth pipeline 29 is connected to the oxidation reactor 6. The fourth electrically controlled valve 30 is arranged on the eighth pipeline 28, and the fourth electrically controlled valve 30 is electrically connected to the control mechanism. And the fifth electrically controlled valve 31 is arranged on the ninth pipeline 29, and the fifth electrically controlled valve 31 is electrically connected to the control mechanism. Among them, the control mechanism can control the opening and closing of the fourth electrically controlled valve 30 and the fifth electrically controlled valve 31 respectively. The thermometer in the oxidation reactor 6 is interlocked with the control mechanism of the fourth electrically-controlled valve 30 and the fifth electrically-controlled valve 31. When the temperature in the oxidation reactor 6 is higher than 900°C, the fourth electrically-controlled valve 30 and the fifth electrically-controlled valve 31 are automatically opened to send the catalyst in the oxidation reactor 6 into the catalyst heat collector 27 for cooling. When the temperature in the oxidation reactor 6 drops to 900°C, the fourth electrically-controlled valve 30 and the fifth electrically-controlled valve 31 are automatically closed.

[0065] In this embodiment, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes: a first gas-solid separator 32 and a second gas-solid separator 36. The first gas-solid separator 32 is arranged on the outside of the reduction reactor 1, and the first gas-solid separator 32 is connected to the reduction reactor 1 through a first recovery pipeline 33 and a second recovery pipeline 34, respectively, and the first gas-solid separator 32 is also connected to the first waste heat recovery heat exchange mechanism 2 through a third recovery pipeline 35. And the second gas-solid separator 36 is arranged on the outside of the oxidation reactor 6, and the second gas-solid separator 36 is connected to the oxidation reactor 6 through a fourth recovery pipeline 37 and a fifth recovery pipeline 38, and the second gas-solid separator 36 is also connected to the second waste heat recovery heat exchange mechanism 7 through a sixth recovery pipeline 39.

[0066] In this embodiment, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a first stripping tower 40 and a second stripping tower 42. The first end of the first stripping tower 40 is connected to the reduction reactor 1 through the second pipeline 10, the second end of the first stripping tower 40 is connected to the oxidation reactor 6 through the second pipeline 10 and the lifting pipeline 9, and the third end of the first stripping tower 40 is connected to the reduction reactor 1 through the tenth pipeline 41. And the first end of the second stripping tower 42 is connected to the reduction reactor 1 through the third pipeline 11, the second end of the second stripping tower 42 is connected to the oxidation reactor 6 through the third pipeline 11, and the third end of the second stripping tower 42 is connected to the oxidation reactor 6 through the eleventh pipeline 43.

[0067] In this embodiment, the solar photothermal catalytic fluidized reaction system for producing hydrogen also includes: a fourth gas supply mechanism 44, a twelfth pipeline 45, a thirteenth pipeline 46 and a fifth flow control valve 47. One end of the twelfth pipeline 45 is connected to the fourth gas supply mechanism 44, and the other end of the twelfth pipeline 45 is connected to the bottom of the second stripping tower 42. One end of the thirteenth pipeline 46 is connected to the twelfth pipeline 45, and the other end of the thirteenth pipeline 46 is connected to the bottom of the first stripping tower 40. And the fifth flow control valve 47 is arranged on the twelfth pipeline 45, and the fifth flow control valve 47 is electrically connected to the control mechanism. Among them, the fourth gas supply mechanism 44 is used to provide the fourth gas to the second stripping tower 42 and the first stripping tower 40 through the twelfth pipeline 45 and the thirteenth pipeline 46 respectively.

[0068] Specifically, the functions of the first stripping tower 40 and the second stripping tower 42 are to replace the reaction products entrained inside the catalyst and between the particles by steam or other suitable gases in a stripping manner; the structures of the first stripping tower 40 and the second stripping tower 42 may be the same or different, for example, the first stripping tower 40 and the second stripping tower 42 both adopt baffle type or grid packing type; wherein the fourth gas may be, for example, steam.

[0069] In this embodiment, the system for producing hydrogen by solar thermal catalytic fluidized reaction also includes a heat exchange mechanism 48, the first end of the heat exchange mechanism 48 is connected to the first stripping tower 40 through the second pipeline 10, the second end of the heat exchange mechanism 48 is connected to the lifting pipeline 9 through the second pipeline 10, the third end of the heat exchange mechanism 48 is connected to the reduction reactor 1 through the third pipeline 11, and the fourth end of the heat exchange mechanism 48 is connected to the second stripping tower 42 through the third pipeline 11.

[0070] Specifically, the heat exchange mechanism 48 is an oxidation-reduction catalyst heat exchanger. In order to improve the utilization rate of light and heat, a device is set up to exchange heat between the oxidation catalyst whose temperature is reduced after the oxidation reaction and the reduction catalyst whose temperature is higher before entering the oxidation reactor 6, which is called the heat exchange mechanism 48. Since both sides of the traditional heat exchanger are gas-solid two-phase media, they are easy to clog and cause abrasion to the inner wall of the equipment. In addition, the temperature of the medium is very high, and the structural type of the heat exchanger must meet the requirements of smooth gas-solid flow, wear resistance, and high temperature resistance. Among them, the heat exchange mechanism 48 can adopt a composite ceramic tube with good thermal conductivity, and its thermal conductivity coefficient is in the range of 0-3000W / mK; wherein, one implementation method of the heat exchange mechanism 48 is to adopt a sleeve-type single-pass, and arrange it in a vertical or inclined manner; wherein, another implementation method of the heat exchange mechanism 48 is to adopt a heat storage structure; wherein, the heat storage heat exchange mechanism 48 is used for catalyst heat exchange between the reduction reactor 1 and the oxidation reactor 6. As Figure 5As shown, the inlet and outlet of the heat storage heat exchange mechanism 48 are respectively provided with two sets of four-way valves 57, which are respectively connected to the two ends of the second pipeline 10 and the third pipeline 11. There are two heat storage heat exchangers 58 in the middle (A / B), one for heating the heat storage material and the other for releasing heat from the heat storage material. The reduction catalyst (1400°C hot flow) goes through the A heat exchanger, and the high-temperature heat storage ceramic (SiC) in the middle is heated. When the temperature reaches the set temperature of 1300-1350°C, or after the heat exchange time is reached, the four-way valve switch is cut off, and the flow in the A heat exchanger is switched to the oxidation catalyst (900°C flow), and the heat storage material in the heat storage heat exchanger 58 releases heat, heating the 900°C catalyst to 950-1000°C, and the heat storage material is cooled, and then the flow is switched again, and so on, and the heat storage heat exchange is performed. Among them, one end of the oxidation catalyst of the first pass of the heat storage heat exchange mechanism 48 is connected to the second stripping tower 42 of the oxidation reactor 6, and the other end is connected to the reduction reactor 1; one end of the reduction catalyst of the other pass of the heat storage heat exchange mechanism 48 is connected to the first stripping tower 40, and the other end is connected to the lifting pipeline 9 through the second pipeline 10 and the second flow control valve 21. As described above, the heat of the high-temperature reduction catalyst is transferred to the low-temperature oxidation catalyst through the heat storage heat exchange mechanism 48, which reduces the heat loss of the entire device and improves the overall light and heat utilization efficiency of the system. The sleeve-type heat exchange mechanism 48 is used for heat exchange of catalysts between the reduction reactor 1 and the oxidation reactor 6. The reduction catalyst (logistics at 1400°C) flows in the inner sleeve, and the oxidation catalyst (logistics at 900°C) flows outside the sleeve. Ribs are respectively arranged inside and outside the sleeve to enhance heat transfer; wherein, the sleeve and ribs are made of GH2747 material, and the 1400°C contact surface is attached with SiC lining to protect the metal material, while the middle high-temperature logistics is cooled from 1400°C to 1300-1350°C, and the low-temperature fluid on the outside is heated from 900°C to 950-1000°C. As described above, the heat of the high-temperature reduction catalyst is transferred to the low-temperature oxidation catalyst through the sleeve-type heat exchange mechanism 48, which reduces the heat loss of the entire device and improves the overall light and heat utilization efficiency of the system.

[0071] In this embodiment, after the first gas is added into the reduction reactor 1 and the first gas fluidizes the catalyst in the reduction reactor 1, the reduction reactor 1 transports the catalyst to the first stripping tower 40, and the fourth gas is added into the first stripping tower 40, so that the catalyst is fluidized in the reduction reactor 1 and the reaction gas between and inside the catalyst particles is stripped and replaced.

[0072] In this embodiment, after the second gas and the third gas are added into the oxidation reactor 6 to fluidize the catalyst in the oxidation reactor 6, the oxidation reactor 6 transports the catalyst to the second stripping tower 42, and adds the fourth gas into the second stripping tower 42, so that the catalyst in the oxidation reactor 6 is fluidized and the reaction gas between and inside the catalyst particles is stripped and replaced.

[0073] In a specific embodiment of the utility model, the working process of the solar thermal catalytic fluidized reaction system for producing hydrogen in actual application is as follows:

[0074] 1. Fluidizing gas (i.e., the first gas, which may be, for example, helium, steam, or a mixture of several gases) is introduced from the utility system (the first gas supply mechanism 4) and injected into the bottom of the reduction reactor 1 through the first pipeline 3. The catalyst is fluidized by a gas distributor arranged in the reduction reactor 1, so that as a reactant, the fluidized catalyst circulates up and down in the reduction reactor 1; wherein the fluidizing gas blown into the distributor fluidizes and stirs the catalyst, thereby increasing the heat transfer and mass transfer efficiency in the reduction reactor 1, thereby maximizing the reaction rate and conversion rate.

[0075] 2. Open the catalyst transfer valve (the first electrically controlled valve 24 and the second electrically controlled valve 25 located on the fifth pipeline 17 and the sixth pipeline 18) between the reduction reactor 1 and the high-temperature heat storage tank 16, and then inject fluidizing gas through the seventh pipeline 19 at the bottom of the high-temperature heat storage tank 16 to allow the catalyst to flow between the high-temperature heat storage tank 16 and the reduction reactor 1.

[0076] 3. Solar thermal energy is introduced from the light-transmitting mirror 15 on the top of the reduction reactor 1 through secondary reflection high-temperature focusing technology (high-temperature focusing mechanism 14), irradiating the catalyst in the reduction reactor 1, heating the temperature of the reduction reactor 1 to 1400°C or above (<1500°C), and the catalyst begins to undergo a reduction reaction to produce oxygen, which is carried out of the reactor by the rapid flow of the fluidizing gas through convective mass transfer. The heating reduction chemical reaction of the metal oxide catalyst is:

[0077]

[0078] 4. When the temperature of the catalyst in the reduction reactor 1 and the high-temperature heat storage tank 16 rises to 1500°C, the first electrically controlled valve 24 and the second electrically controlled valve 25 on the fifth pipeline 17 and the sixth pipeline 18 between the reduction reactor 1 and the high-temperature heat storage tank 16 are closed, so that the high-temperature heat storage tank 16 can store the catalyst after high-temperature reduction for standby use, and provide heat for the entire system at night or when there is no sunlight, so as to ensure that the system can produce continuously.

[0079] 5. Synchronously open the second flow control valve 21 (for example, a slide valve, a plug valve, etc.) on the second pipeline 10 between the reduction reactor 1 and the oxidation reactor 6. The reduced catalyst will carry the first mixed gas, so the reduced catalyst is separated from the first mixed gas through the stripping tower. The first mixed gas returns to the reduction reactor 1 through the tenth pipeline 41, and the separated reduced catalyst is introduced into the lifting pipeline 9 after heat exchange by the heat exchange mechanism 48, and the opening of the second flow control valve 21 is adjusted according to the production volume to control the flow of the reduced catalyst. At the same time, open the sixth flow control valve 5 between the second gas supply mechanism 8 and the lifting pipeline 9, and inject the second gas into the bottom of the lifting pipeline 9. The second gas can be, for example, superheated steam (from a 0.5MPa steam network) to transport the reduced catalyst in the lifting pipeline 9 to the stripping tower. The third gas enters from the bottom of the oxidation reactor 6 through the gas distributor (i.e., the third gas supply mechanism 12 injects the third gas into the bottom of the oxidation reactor 6 through the fourth pipeline 13, and the fourth pipeline 13 is provided with a fourth flow control valve 23. The oxidation reactor 6 and the reduction reactor 1 are selected from metal oxides (M x O y ) is a catalyst, the metal oxide may be selected from metals including iron, nickel, copper, magnesium, manganese, zinc, cobalt, cerium, etc., alumina Al2O3 is a carrier, the average particle diameter is about 100μm to 200μm, the micropore diameter is 3nm to 6nm, and the specific surface area is 200m 2 / g~250m 2 / g. The atomic layer deposition method is used to evenly distribute the catalyst on the inner and outer surfaces of the carrier at the atomic layer height to increase the specific surface area of ​​the reaction contact. The ratio of the metal oxide catalyst to the carrier is determined according to the molecular weight of different metals and the amount of hydrogen produced, and the ratio ranges from 5% to 50%. Among them, the physical and chemical properties of the catalyst are as follows:

[0080] project nature <![CDATA[Heap ratio, kg / m 3 > 800-1000 <![CDATA[Specific surface area, m 2 / g]]> 200-250 Wear resistance index ＜3 Average particle size, μm 100-200

[0081] 6. The reduced catalyst enters from the lower part of the oxidation reactor 6, and the third gas enters from the bottom of the oxidation reactor 6. The reduced catalyst and the gas phase reactant (water vapor / third gas mixed gas) in the oxidation reactor 6 flow in reverse, which enhances the contact mass transfer and heat transfer effect between the medium and the reduced catalyst, and increases the oxidation reaction speed. The chemical reaction balance is:

[0082] M x O y-δ +δH2O→M x O y +δH2

[0083] 7. Synchronously open the third flow control valve 22 (for example, a slide valve, a plug valve, etc.) on the third pipeline 11 between the oxidation reactor 6 and the reduction reactor 1. The oxidation catalyst can carry the second mixed gas, so the oxidation catalyst is separated from the second mixed gas through a stripping tower, and the second mixed gas returns to the oxidation reactor 6 through an eleventh pipeline 43. The separated oxidation catalyst utilizes the pressure difference between the oxidation reactor 6 and the reduction reactor 1 to firstly undergo heat exchange through the heat exchange mechanism 48, and then the oxidized catalyst is returned to the lower part of the reduction reactor 1. The second flow control valve 21 is used to control the storage of the oxidation reactor 6, thereby achieving a balance in the inlet and outlet flow of the fluidized catalyst in the oxidation reactor 6 and the reduction reactor 1.

[0084] 8. A catalyst heat collector 27 is provided outside the oxidation reactor 6 to control the temperature of the oxidation reactor 6 (~900°C) by cooling the catalyst and recover the heat inside the oxidation reactor 6 to generate steam. The water vapor pressure can be selected within the range of 1.0MPa to 10MPa as required.

[0085] 9. The second mixed gas (mixed gas of hydrogen and water vapor) generated by the oxidation reactor 6 enters the second gas-solid separator 36 outside the oxidation reactor 6 through the fourth recovery pipeline 37 to separate and recover the catalyst. The separated solid (catalyst) returns to the oxidation reactor 6 through the fifth recovery pipeline 38, and the second mixed gas is discharged from the top and enters the subsequent second waste heat recovery heat exchange mechanism 7 through the sixth recovery pipeline 39. The hydrogen recovered by the second waste heat recovery heat exchange mechanism 7 is dried and discharged from the device; wherein, the second waste heat recovery heat exchange mechanism 7 is as follows Figure 4 shown.

[0086] 10. The first mixed gas (a mixed gas of hydrogen and fluidizing gas) at the outlet of the reduction reactor 1 enters the first gas-solid separator 32 outside the reduction reactor 1 through the first recovery pipeline 33 for separation. The separated solid (catalyst) returns to the reduction reactor 1 through the second recovery pipeline 34, and the first mixed gas is discharged from the top and enters the subsequent first waste heat recovery heat exchange mechanism 2 through the third recovery pipeline 35. The mixed gas after cooling (~40°C), if helium is used as the fluidizing gas (first gas), is recycled by pressure swing adsorption (PSA) to recover the fluidizing gas, and then is dried with oxygen and then discharged from the device. The structure of the first waste heat recovery heat exchange mechanism 2 using helium as the fluidizing gas (first gas) is as shown in FIG. Figure 2 As shown. The mixed gas using steam as the fluidizing gas (first gas) is cooled (~40°C) and the condensed water is recovered through the first waste heat recovery heat exchange mechanism 2 (as shown Figure 3 Steam recycling occurs as shown).

[0087] 11. The product yield may be, for example:

[0088] Hydrogen product flow rate 1316kg / h (>99.999%)

[0089] Oxygen product flow rate 10526kg / h (>99.999%)

[0090] Raw material flow rate H2O 11842kg / h

[0091] Solar thermal input 294MW

[0092] Heat recovery

[0093] Output high pressure steam 217000kg / h

[0094] Output medium pressure steam 167000kg / h

[0095] Energy efficiency>50%.

[0096] In summary, this embodiment uses a photothermal method, a catalyst and a reducing agent to generate hydrogen from water to provide the production of sustainable renewable fuels (including sustainable aviation fuels, Sustainable Aviation Fuel) or chemical synthesis raw materials (including methanol, etc.). The solar energy intensity is increased by using a solar concentrating system, and the concentration ratio reaches 5000-8000 times, providing a heat source with high temperature and high energy density. This technology can greatly improve the utilization efficiency of solar energy and provide the required thermal energy for the thermochemical hydrogen production process. By using solar energy and water vapor as raw materials, the solar thermochemical catalytic fluidized reaction hydrogen production technology can achieve an efficient energy conversion process. The optimization of the catalyst and fluidized reactor design of the thermochemical reaction can increase the hydrogen production to an industrial scale and improve the energy utilization efficiency. The oxidation reactor 6 and the reduction reactor 1 are arranged in parallel, and the operating pressure of the reduction reactor 1 is very low. It is arranged at a high place, which is not only the need for catalyst delivery pressure balance, but also convenient for receiving the high temperature radiation energy of the concentrating system. The catalyst enters the reactor by gravity.

[0097] In summary, the solar thermal catalytic fluidized reaction system for producing hydrogen of the utility model is low-carbon and environmentally friendly, and can industrially produce hydrogen for producing sustainable renewable fuels or chemical synthesis raw materials, and improves energy utilization efficiency.

[0098] Note that the above are only preferred embodiments of the present invention and the technical principles used. Those skilled in the art will understand that the present invention is not limited to the specific embodiments described herein, and that various obvious changes, readjustments and substitutions can be made by those skilled in the art without departing from the scope of protection of the present invention. Therefore, although the present invention is described in more detail through the above embodiments, the present invention is not limited to the above embodiments, and may include more other equivalent embodiments without departing from the concept of the present invention, and the scope of the present invention is determined by the scope of the appended claims.

Claims

1. A system for producing hydrogen by solar thermal catalytic fluidized reaction, characterized in that: include: A reduction reactor having a catalyst therein, and the reduction reactor is used to reduce the catalyst to obtain a reduced catalyst and a first mixed gas; A first waste heat recovery and heat exchange mechanism is disposed outside the reduction reactor, and the first waste heat recovery and heat exchange mechanism is used to receive the first mixed gas and generate oxygen; a first pipeline, one end of which is connected to the bottom of the reduction reactor; A first gas supply mechanism is connected to the other end of the first pipeline, and the first gas supply mechanism is used to provide a first gas to the reduction reactor, so as to fluidize the catalyst and serve as a reactant; An oxidation reactor, used for oxidizing the reduced catalyst to obtain the catalyst and a second mixed gas; a second gas supply mechanism connected to the oxidation reactor via a lifting pipeline, and the second gas supply mechanism is used to provide a second gas to the oxidation reactor; a second pipeline, one end of which is connected to the reduction reactor, and the other end of which is connected to the lifting pipeline; a third pipeline, one end of which is connected to the oxidation reactor, and the other end of which is connected to the reduction reactor; The second waste heat recovery and heat exchange mechanism is arranged outside the oxidation reactor, and the second waste heat recovery and heat exchange mechanism is used to receive the second mixed gas and generate hydrogen.

2. The system for producing hydrogen by solar thermal catalytic fluidized reaction according to claim 1, characterized in that: Also includes: The third gas supply mechanism is connected to the bottom of the oxidation reactor through a fourth pipeline, and the third gas supply mechanism is used to provide a third gas to the oxidation reactor for fluidization and as a reactant.

3. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 2, characterized in that: Also includes: High temperature concentrating mechanism for providing solar heat; as well as A light-transmitting mirror is arranged on the top of the reduction reactor, and is used to receive the solar light heat provided by the high-temperature focusing mechanism and introduce the solar light heat into the reduction reactor, thereby heating the reduction reactor.

4. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 3, characterized in that: Also includes: A high-temperature heat storage tank, wherein the high-temperature heat storage tank is connected to the reduction reactor through a fifth pipeline and a sixth pipeline respectively; as well as A seventh pipeline, one end of the seventh pipeline is connected to the bottom of the high-temperature heat storage tank, and the other end of the seventh pipeline is connected to the first pipeline.

5. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 4, characterized in that: Also includes: Controlling bodies; a first flow control valve, disposed on the first pipeline, and the first flow control valve is electrically connected to the control mechanism; a second flow control valve, disposed on the second pipeline, and the second flow control valve is electrically connected to the control mechanism; a third flow control valve, disposed on the third pipeline, and the third flow control valve is electrically connected to the control mechanism; a fourth flow control valve, disposed on the fourth pipeline, and the fourth flow control valve is electrically connected to the control mechanism; a first electrically controlled valve, disposed on the fifth pipeline, and electrically connected to the control mechanism; a second electrically controlled valve, disposed on the sixth pipeline, and the second electrically controlled valve is electrically connected to the control mechanism; as well as a third electrically-controlled valve, disposed on the seventh pipeline, and the third electrically-controlled valve is electrically connected to the control mechanism; Among them, the control mechanism can control the opening and closing of the first flow control valve, the second flow control valve, the third flow control valve, the fourth flow control valve, the first electrically-controlled valve, the second electrically-controlled valve and the third electrically-controlled valve respectively.

6. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 5, characterized in that: Also includes: A catalyst heat collector is arranged outside the oxidation reactor; an eighth pipeline, one end of which is connected to the bottom of the catalyst heat collector, and the other end of which is connected to the oxidation reactor; a ninth pipeline, one end of which is connected to the upper portion of the catalyst heat collector, and the other end of which is connected to the oxidation reactor; a fourth electrically-controlled valve, disposed on the eighth pipeline, and the fourth electrically-controlled valve is electrically connected to the control mechanism; and a fifth electrically-controlled valve, disposed on the ninth pipeline, and electrically connected to the control mechanism; Wherein, the control mechanism can control the opening and closing of the fourth electrically-controlled valve and the fifth electrically-controlled valve respectively.

7. The system for producing hydrogen by solar thermal catalytic fluidized reaction according to claim 1, characterized in that: Also includes: a first gas-solid separator, disposed outside the reduction reactor, the first gas-solid separator being connected to the reduction reactor through a first recovery pipeline and a second recovery pipeline, respectively, and the first gas-solid separator being further connected to the first waste heat recovery and heat exchange mechanism through a third recovery pipeline; and The second gas-solid separator is arranged outside the oxidation reactor, and the second gas-solid separator is connected to the oxidation reactor through a fourth recovery pipeline and a fifth recovery pipeline, and the second gas-solid separator is also connected to the second waste heat recovery heat exchange mechanism through a sixth recovery pipeline.

8. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 5, characterized in that: Also includes: a first stripping tower, wherein a first end of the first stripping tower is connected to the reduction reactor via the second pipeline, a second end of the first stripping tower is connected to the oxidation reactor via the second pipeline and the lifting pipeline, and a third end of the first stripping tower is connected to the reduction reactor via a tenth pipeline; as well as A second stripping tower, wherein the first end of the second stripping tower is connected to the reduction reactor through the third pipeline, the second end of the second stripping tower is connected to the oxidation reactor through the third pipeline, and the third end of the second stripping tower is connected to the oxidation reactor through an eleventh pipeline.

9. The system for producing hydrogen by solar thermal catalytic fluidized reaction as claimed in claim 8, characterized in that: Also includes: a fourth gas supply mechanism; a twelfth pipeline, one end of which is connected to the fourth gas supply mechanism, and the other end of which is connected to the bottom of the second stripping tower; a thirteenth pipeline, one end of the thirteenth pipeline is connected to the twelfth pipeline, and the other end of the thirteenth pipeline is connected to the bottom of the first stripping tower; and a fifth flow control valve, disposed on the twelfth pipeline, and the fifth flow control valve is electrically connected to the control mechanism; The fourth gas supply mechanism is used to provide the fourth gas to the second stripping tower and the first stripping tower through the twelfth pipeline and the thirteenth pipeline respectively.

10. The system for producing hydrogen by solar thermal catalytic fluidized reaction according to claim 8, characterized in that: It also includes a heat exchange mechanism, a first end of the heat exchange mechanism is connected to the first stripping tower through the second pipeline, a second end of the heat exchange mechanism is connected to the lifting pipeline through the second pipeline, a third end of the heat exchange mechanism is connected to the reduction reactor through the third pipeline, and a fourth end of the heat exchange mechanism is connected to the second stripping tower through the third pipeline.

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