A device and method for hydrogen production by in-situ carbon capture of biomass driven by microwave

Abstract

The application provides a device and method for hydrogen production by in-situ carbon capture of biomass driven by microwaves, which comprises a pyrolysis reactor, a catalytic adsorption reactor, a condensing device and a gas dryer, and the pyrolysis reactor is connected with a first microwave generator. The catalytic adsorption reactor is used for adsorbing carbon dioxide in pyrolysis gas, the gas inlet of the catalytic adsorption reactor is connected with the gas outlet of the pyrolysis reactor, and the catalytic adsorption reactor is connected with a second microwave generator. The condensing device is connected with the gas outlet of the catalytic adsorption reactor, so as to separate tar in hydrogen by condensation. The gas inlet of the gas dryer is connected with the gas outlet of the condensing device, so as to remove water in hydrogen. The application can make the catalytic reaction and CO2 adsorption synchronously carried out in the same reactor, remove CO2 in-situ while hydrogen is produced, simplify the process flow, directly output hydrogen with high purity, reduce the energy consumption and cost of subsequent separation, and improve the hydrogen production efficiency of biomass.

Description

Technical Field

[0001] This invention relates to the fields of biomass energy utilization and CO2 in-situ carbon capture technology, and particularly to a microwave-driven biomass in-situ carbon capture hydrogen production device and method. Background Technology

[0002] Biomass, as a renewable, low-carbon, and clean energy source, is considered an important way to replace fossil fuels and promote sustainable development. It fixes carbon dioxide through photosynthesis and possesses natural carbon-neutral properties. Developing carbon-neutral fuels such as H2 and syngas using biomass as a raw material is of great significance for alleviating the energy crisis and achieving carbon cycle and carbon neutrality goals.

[0003] Among numerous biomass conversion technologies, gasification for hydrogen production has attracted much attention due to its superior product quality, high conversion efficiency, and wide adaptability to feedstocks. However, the purity of hydrogen obtained from conventional biomass gasification is typically only 30% to 50%, and the syngas contains large amounts of tar, CO, and CO2, leading to high costs and significant energy consumption in subsequent purification and separation processes. Summary of the Invention

[0004] This invention aims to at least partially solve one of the technical problems in related technologies. To this end, embodiments of this invention provide a microwave-driven biomass in-situ carbon capture and hydrogen production device and method, which removes CO2 in situ while producing hydrogen, simplifying the process and reducing energy consumption and costs for subsequent separation.

[0005] One embodiment of the present invention provides a microwave-driven biomass in-situ carbon capture and hydrogen production device, comprising: a pyrolysis reactor, a catalytic adsorption reactor, a condensation device and a gas dryer. The pyrolysis reactor has an inlet and an outlet. The inlet of the pyrolysis reactor is used to introduce a mixture of inert gas and water vapor into the pyrolysis reactor. The pyrolysis reactor is connected to a first microwave generator.

[0006] The catalytic adsorption reactor is used to adsorb carbon dioxide from pyrolysis gas. The catalytic adsorption reactor has an inlet and an outlet. The inlet of the catalytic adsorption reactor is connected to the outlet of the pyrolysis reactor. The catalytic adsorption reactor is connected to a second microwave generator.

[0007] The inlet of the condenser is connected to the outlet of the catalytic adsorption reactor to separate the tar from the hydrogen through condensation.

[0008] The gas dryer's inlet is connected to the condenser's outlet to remove moisture from the hydrogen.

[0009] In some embodiments, the pyrolysis reactor is located above the catalytic adsorption reactor, and the exhaust port of the pyrolysis reactor is connected to the inlet of the catalytic adsorption reactor by a connecting pipe. A first baffle is connected to the bottom of the pyrolysis reactor, and a second baffle is connected to the bottom of the catalytic adsorption reactor. The first baffle and the second baffle each have a plurality of gas passage holes for gas flow.

[0010] In some embodiments, the microwave-driven biomass in-situ carbon capture and hydrogen production device further includes a gas mixer having a first inlet, a second inlet, and an outlet. The first inlet of the gas mixer is connected to an inert gas source, the second inlet of the gas mixer is connected to a steam generator, and the outlet of the gas mixer is connected to the gas inlet of the pyrolysis reactor.

[0011] In some embodiments, the outlet of the gas mixer is connected to the inlet of the pyrolysis reactor via a heat tracing pipe made of quartz, and the outside of the pipe is connected with a heat tracing cable.

[0012] In some embodiments, a liquid injection pump is connected to the inlet of the steam generator.

[0013] In some embodiments, the pyrolysis reactor is connected to a first non-contact infrared thermometer, which is electrically connected to a first microwave generator, and the catalytic adsorption reactor is connected to a second non-contact infrared thermometer, which is electrically connected to a second microwave generator.

[0014] In some embodiments, the microwave-driven biomass in-situ carbon capture and hydrogen production device further includes a gas chromatography-mass spectrometry (GC-MS) instrument connected to the outlet of a gas dryer to analyze the composition and concentration of the final gaseous product online.

[0015] Another embodiment of the present invention proposes a microwave-driven in-situ carbon capture and hydrogen production method for biomass, which utilizes the aforementioned microwave-driven in-situ carbon capture and hydrogen production device and includes the following steps: S1. Place biomass and microwave absorber in a pyrolysis reactor, and place microwave-absorbing-catalytic bifunctional material and carbon dioxide adsorbent in a catalytic adsorption reactor; S2. Purge the pyrolysis reactor and the catalytic adsorption reactor with inert gas; S3. Inert gas and water vapor are introduced into the pyrolysis reactor and the catalytic adsorption reactor, and the first microwave generator and the second microwave generator are turned on at the same time. S4. The pyrolysis gas generated in the pyrolysis reactor enters the catalytic adsorption reactor to remove carbon dioxide from the pyrolysis gas. S5. The pyrolysis gas with carbon dioxide removed is passed into a condenser to separate the tar from the pyrolysis gas. After the tar-removed gas is dehydrated by a gas dryer, hydrogen is obtained.

[0016] In some embodiments, in step S1, after the biomass and the microwave absorber are uniformly mixed, they are placed in a pyrolysis reactor, and the microwave absorber accounts for 10% to 50% of the total mass of the biomass and the microwave absorber.

[0017] In some embodiments, in step S1, the absorption... The catalytic bifunctional material and carbon dioxide adsorbent are packed in a layered manner, with the microwave absorbing material being the core component. The catalytic bifunctional material is positioned above the carbon dioxide adsorbent, and the amount of carbon dioxide adsorbent added is [amount missing - likely a specific concentration]. The mass of the catalytic bifunctional material is 1 to 5 times that of the catalytic bifunctional material. Attached Figure Description

[0018] The above and / or additional aspects and advantages of the present invention will become apparent and readily understood from the following description of the embodiments taken in conjunction with the accompanying drawings. in: Figure 1 This is a schematic diagram of the structure of a microwave-driven biomass in-situ carbon capture and hydrogen production device according to an embodiment of the present invention. Figure label: 1. Inert gas source; 2. Mass flow controller; 3. Liquid injection pump; 4. Steam generator; 5. Gas mixer; 6. Heat tracing pipe; 7. First microwave generator; 8. Second microwave generator; 9. Condensation device; 10. Pyrolysis reactor; 11. First partition; 12. Catalytic adsorption reactor; 13. Second partition; 14. Connecting pipe; 15. Heat tracing tape; 16. First non-contact infrared thermometer; 17. Second non-contact infrared thermometer; 18. Gas chromatography-mass spectrometry; 19. Gas dryer. Detailed Implementation

[0019] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0020] The microwave-driven biomass in-situ carbon capture and hydrogen production apparatus and method of the present invention are described below with reference to the accompanying drawings.

[0021] like Figure 1As shown, one embodiment of the present invention proposes a microwave-driven biomass in-situ carbon capture and hydrogen production device, comprising: a pyrolysis reactor 10, a catalytic adsorption reactor 12, a condenser 9, and a gas dryer 19. The pyrolysis reactor 10 has an inlet and an outlet. The inlet of the pyrolysis reactor 10 is used to introduce a mixture of inert gas and water vapor into the pyrolysis reactor 10. The pyrolysis reactor 10 is connected to a first microwave generator 7. The catalytic adsorption reactor 12 is used to adsorb carbon dioxide from the pyrolysis gas. The catalytic adsorption reactor 12 has an inlet and an outlet. The inlet of the catalytic adsorption reactor 12 is connected to the outlet of the pyrolysis reactor 10. The catalytic adsorption reactor 12 is connected to a second microwave generator 8. The inlet of the condenser 9 is connected to the outlet of the catalytic adsorption reactor 12 to separate tar from the hydrogen gas by condensation. The inlet of the gas dryer 19 is connected to the outlet of the condenser 9 to remove moisture from the hydrogen gas.

[0022] This invention, by placing a catalytic adsorption reactor 12 downstream of the pyrolysis reactor 10, allows the catalytic reaction and CO2 adsorption to occur simultaneously within the same reactor. This enables in-situ CO2 removal while producing hydrogen, simplifying the process and directly outputting high-purity hydrogen. It also reduces energy consumption and costs in subsequent separation, thus improving the hydrogen production efficiency of biomass. A condensation device separates tar and other liquid substances from the hydrogen through condensation. A gas dryer removes moisture from the hydrogen.

[0023] Furthermore, both the first microwave generator 7 and the second microwave generator 8 have independent dual power output terminals, enabling independent heating and temperature control in different zones. The transmission frequency of both is 2.45 GHz, and the output power of a single zone is continuously adjustable within the range of 200~1500 W.

[0024] Furthermore, the pyrolysis reactor 10 is located within the first microwave resonant cavity, and the first microwave generator 7 is connected to the first microwave resonant cavity. The catalytic adsorption reactor 12 is located within the second microwave resonant cavity, and the second microwave generator 8 is connected to the second microwave resonant cavity. This allows microwave energy to heat the reactors efficiently and rapidly.

[0025] Furthermore, the interior of the gas dryer 19 is filled with a desiccant.

[0026] In some embodiments, the pyrolysis reactor 10 is disposed above the catalytic adsorption reactor 12, and the exhaust port of the pyrolysis reactor 10 and the inlet of the catalytic adsorption reactor 12 are connected by a connecting pipe 14. A first baffle 11 is connected to the bottom of the pyrolysis reactor 10, and a second baffle 13 is connected to the bottom of the catalytic adsorption reactor 12. The first baffle 11 and the second baffle 13 each have a plurality of gas passage holes for gas flow.

[0027] Furthermore, the material in the pyrolysis reactor 10 is loaded above the first partition 11, and the material in the catalytic adsorption reactor 12 is loaded above the second partition 13.

[0028] It should be noted that the material in the pyrolysis reactor 10 will not clog the vent holes of the first partition 11, and the material in the catalytic adsorption reactor 12 will not clog the vent holes of the second partition 13. This is because the material in the pyrolysis reactor 10 includes biomass and microwave absorbers. The biomass is in a loose state, while the microwave absorber is granular. After being mixed and stacked, they have pores. During the pyrolysis process, the biomass forms a loose and porous structure, allowing the generated gas to pass smoothly through the first partition 11 into the catalytic adsorption reactor 12. The material in the catalytic adsorption reactor 12 includes microwave-absorbing-catalytic dual-functional materials and carbon dioxide adsorbents. After these materials are stacked, they have pores, allowing gas to enter through the pores and pass through the second partition 13. Alternatively, a certain amount of space can be reserved when stacking the materials to allow the gas to pass smoothly.

[0029] Furthermore, the materials in both the pyrolysis reactor 10 and the catalytic adsorption reactor 12 are loaded into the effective heating area of ​​the microwave waveguide.

[0030] Furthermore, both the pyrolysis reactor 10 and the catalytic adsorption reactor 12 are vertically oriented tubular structures, coaxially arranged in the vertical direction. The pipe diameter can be 20~25 mm, and the wall thickness can be 1.5~2.5 mm. Depending on the processing scale, reactors of other sizes can also be used. The first baffle 11 and the second baffle 13 allow the reactant gas to pass through the material layer vertically, greatly improving the heat and mass transfer efficiency between the gas and solid phases.

[0031] Furthermore, the material bed height of the pyrolysis reactor 10 and the catalytic adsorption reactor 12 is 40~50 mm, for example, about 43 mm.

[0032] In some embodiments, the microwave-driven biomass in-situ carbon capture and hydrogen production device further includes a gas mixer 5, which has a first inlet, a second inlet and an outlet. The first inlet of the gas mixer 5 is connected to an inert gas source 1, the second inlet of the gas mixer 5 is connected to a steam generator 4, and the outlet of the gas mixer 5 is connected to the gas inlet of the pyrolysis reactor 10.

[0033] Furthermore, the inert gas source 1 is high-purity nitrogen or argon, stored in steel cylinders. The role of the inert gas is to provide an oxygen-free reaction atmosphere and drive the flow of the reaction gas.

[0034] Furthermore, a mass flow controller 2 is connected to the connecting pipe 14 between the first inlet of the gas mixer 5 and the inert gas source 1 to regulate the flow rate of the inert gas, typically controlling it to 50~100 mL / min.

[0035] In some embodiments, the outlet of the gas mixer 5 is connected to the inlet of the pyrolysis reactor 10 via a heat tracing pipe 6. The connecting pipe 14 is made of quartz, and a heat tracing cable 15 is connected to the outside of the connecting pipe 14. The temperature control range of the heat tracing pipe 6 and the heat tracing cable 15 can be maintained at 150~200 °C, which is intended to prevent water vapor and heavy component pyrolysis intermediate products from condensing during transportation.

[0036] In some embodiments, the inlet of the steam generator 4 is connected to a liquid injection pump 3, which is used to deliver deionized water to the steam generator 4. This allows for precise control of the amount of water injected into the steam generator 4, thereby enabling dynamic and precise adjustment of the water-carbon ratio within the system.

[0037] In some embodiments, the pyrolysis reactor 10 is connected to a first non-contact infrared thermometer 16, which is electrically connected to a first microwave generator 7. The catalytic adsorption reactor 12 is connected to a second non-contact infrared thermometer 17, which is electrically connected to a second microwave generator 8. The non-contact infrared thermometers are used to monitor the reaction temperature in real time and feed it back to the microwave generator, forming a closed-loop control to precisely adjust the output power. This allows for precise control of the temperatures of the pyrolysis reactor 10 and the catalytic adsorption reactor 12, maintaining the pyrolysis reactor 10 at a medium temperature and the catalytic adsorption reactor 12 at a medium-high temperature. This solves the technical contradiction that a single temperature cannot simultaneously achieve optimal reaction conditions for multiple processes.

[0038] In some alternative embodiments, the non-contact infrared thermometer can be replaced by a thermocouple inserted into the reactor, such as a type K thermocouple, as long as it can meet the measurement requirements of the reaction temperature range of 200~1000 °C.

[0039] In some embodiments, the microwave-driven biomass in-situ carbon capture and hydrogen production device further includes a gas chromatography-mass spectrometry (GC-MS) instrument 18, which is connected to the outlet of a gas dryer 19 to analyze the composition and concentration of the final gaseous product online.

[0040] The Gas Chromatography-Mass Spectrometer 18 is used for quantitative analysis of H2, CO, CO2 and light hydrocarbons such as CH4, C2H4 and C2H6 gases. Its analytical range is 0~100%, its resolution is 0.01%, and its relative measurement error does not exceed 2%.

[0041] Furthermore, the gas chromatograph-mass spectrometer 18 has a time resolution of 0.1~5s for analyzing the exhaust gas components, such as 0.5s, 1s, 2s, 3s, etc., to achieve dynamic monitoring of the exhaust gas components and the reaction process.

[0042] It should be noted that the outlet of the gas dryer 19 is connected to the exhaust pipe, and the other end of the exhaust pipe is a gas collection device. The gas chromatograph-mass spectrometer 18 is connected to the exhaust pipe as a branch to realize dynamic monitoring of the exhaust gas components and reaction process.

[0043] Another embodiment of the present invention proposes a microwave-driven in-situ carbon capture and hydrogen production method for biomass, which utilizes the aforementioned microwave-driven in-situ carbon capture and hydrogen production device and includes the following steps: S1. Place biomass and microwave absorber in pyrolysis reactor 10, and place microwave absorber-catalyst bifunctional material and carbon dioxide adsorbent in catalytic adsorption reactor 12; S2. Inert gas is introduced into the pyrolysis reactor 10 and the catalytic adsorption reactor 12 for purging, so that an inert atmosphere is formed in the pyrolysis reactor 10 and the catalytic adsorption reactor 12. S3. Inert gas and water vapor are introduced into the pyrolysis reactor 10 and the catalytic adsorption reactor 12. At the same time, the first microwave generator 7 and the second microwave generator 8 are turned on, and the heating function of the heat tracing pipe 6 and the heat tracing tape 15 is activated. The microwave power of the first microwave generator 7 and the second microwave generator 8 are adjusted respectively to rapidly raise the temperature of the pyrolysis reactor 10 to 500~800℃, generating pyrolysis gas and volatiles. The biomass pyrolysis reaction occurs in the pyrolysis reactor 10, and its chemical reaction formula is as follows:

[0044] S4. The pyrolysis gas generated in the pyrolysis reactor 10 is carried by the carrier gas (i.e., inert gas) and enters the catalytic adsorption reactor 12 through the connecting pipe 14 to remove carbon dioxide from the pyrolysis gas; the temperature of the catalytic adsorption reactor 12 is maintained at the temperature required for both catalytic reaction and CO2 adsorption.

[0045] In the catalytic adsorption reactor 12, both the water-gas shift reaction of tar and the CO2 capture reaction by the carbon dioxide adsorbent occur simultaneously. The chemical reaction formula is as follows:

[0046] S5. The pyrolysis gas, after carbon dioxide removal, is passed into the condenser 9 to separate the tar from the pyrolysis gas. The tar-removed gas is then dehydrated by the gas dryer 19 to obtain hydrogen. The generated hydrogen is analyzed in real time using a gas chromatograph-mass spectrometer 18.

[0047] In this embodiment of the invention, the catalytic adsorption reactor 12 is filled with a microwave absorbing material. The combination of catalytic bifunctional materials and carbon dioxide adsorbents enables the high-value conversion of biomass while reducing the carbon footprint of hydrogen production. Moreover, this integrated design avoids the need for a separate carbon capture system, significantly reducing the high costs and energy consumption of traditional carbon capture, compression, and transportation processes.

[0048] The method provided in this invention addresses the problems of low hydrogen purity and large amounts of tar and CO / CO2 in the syngas produced from biomass. By spatially separating biomass pyrolysis and tar catalytic reforming, and integrating CO2 in-situ adsorption downstream, it achieves efficient hydrogen production and carbon capture in one integrated manner.

[0049] It should be noted that microwave absorbing agents refer to media whose main function is to absorb microwaves and promote the rapid pyrolysis of biomass; microwave absorbing-catalyzing dual-functional materials refer to composite materials that simultaneously possess efficient microwave absorption capabilities and catalytic reforming reaction activity.

[0050] Furthermore, the microwave absorbing agent is one or more of activated carbon, biochar, or silicon carbide.

[0051] Furthermore, the microwave absorption-catalysis bifunctional material is a transition metal catalyst supported on a carbon support, ceramic support, or zeolite support, wherein the transition metal is an alloy composed of one or two of iron, nickel, and copper.

[0052] Furthermore, the carbon dioxide adsorbent is one of calcium oxide, hydrotalcite-based adsorbent, or lithium silicate.

[0053] Furthermore, biomass can be selected from energy crops or agricultural residues with a high hydrogen-to-carbon ratio and a low oxygen-to-carbon ratio, including but not limited to herbaceous energy crops, woody energy crops and their processing residues, such as rice straw.

[0054] Furthermore, prior to step S1, the biomass undergoes drying and grinding. Specifically, the drying temperature is set to 80~120 ℃, the drying time is set to 24 h, and the material is ground and sieved until the particle size is less than 200 μm.

[0055] In some embodiments, in step S1, after the biomass and the microwave absorber are uniformly mixed, they are placed in the pyrolysis reactor 10, and the microwave absorber accounts for 10% to 50% of the total mass of the biomass and the microwave absorber.

[0056] In some embodiments, in step S1, the absorption... The catalytic bifunctional material and carbon dioxide adsorbent are packed in a layered manner, with the microwave absorbing material being the core component. The catalytic bifunctional material is positioned above the carbon dioxide adsorbent, and the amount of carbon dioxide adsorbent added is [amount missing - likely a specific concentration]. The mass of the catalytic bifunctional material is 1 to 5 times that of the catalytic bifunctional material.

[0057] Furthermore, wave absorption Catalytic bifunctional materials can be prepared by methods known in the art, such as impregnation and hydrothermal methods.

[0058] The present invention will be further illustrated by specific embodiments below.

[0059] Example 1 Microwave-driven in-situ carbon capture and hydrogen production based on rice straw.

[0060] (1) Material pretreatment and reactor loading: Rice straw was vacuum dried at 105 °C for 24 h and then pulverized through a 100-mesh sieve. Activated carbon, the microwave absorber, was vacuum dried at 105 °C for 24 h and then ground to a particle size of <200 μm. The mixture of dried rice straw and treated activated carbon was mixed at a mass ratio of 1:0.2 and loaded into the first partition 11 of the pyrolysis reactor 10. Ni / activated carbon microwave absorber-catalyst bifunctional material loaded with 10 wt% nickel was prepared by impregnation and mixed with CO2 adsorbent CaO at a mass ratio of 1:3 and loaded into the second partition 13 of the catalytic adsorption reactor 12.

[0061] (2) System purging and reaction gas introduction: Turn on the gas-liquid supply module and introduce nitrogen gas at a flow rate of 50 mL / min to purge the reactor and pipelines for 30 min to remove air. Introduce water vapor into the system through the steam generator 4 at a water inlet rate of 0.5 mL / min, which is carried into the reaction zone by the nitrogen gas. At the same time, turn on the heat tracing cable 15 and the heat tracing pipe 6 of the connecting pipe 14 and maintain it at 150°C to prevent water vapor and tar from condensing during transportation.

[0062] (3) Microwave start-up and pyrolysis reaction: Adjust the first microwave generator 7 and the second microwave generator 8 respectively, and set the initial power to 300W. Adjust the microwave power of the pyrolysis reactor 10 to 600W, raise the temperature to 600℃, and maintain the reaction at this temperature for 30 min to allow the rice straw to undergo pyrolysis.

[0063] (4) Catalytic reforming and in-situ CO2 adsorption: The microwave power of the catalytic adsorption reactor 12 is adjusted to 800 W, and the temperature is maintained at 800℃. The pyrolysis gas enters the zone under the carry-on of nitrogen, and undergoes tar catalytic reforming and steam reforming reactions under the action of Ni / activated carbon catalyst. At the same time, the CaO adsorbent captures the CO2 generated in the reaction in situ, generating CaCO3, which pushes the reaction equilibrium towards hydrogen production.

[0064] (5) Product Collection and Online Analysis: The gas stream after the reaction passes through a serpentine condenser 9 to collect liquid tar and water. The gaseous products are dehydrated by a gas dryer 19 to obtain hydrogen-rich gas. The hydrogen-rich gas is analyzed in real time (H2, CO, CH4, etc.) using a gas chromatograph-mass spectrometer 18. After the reaction is completed, the solid residues from the two reactors are collected for characterization.

[0065] It should be noted that the hydrogen produced may contain trace amounts of impurity combustible gases such as CO and CH4. By using the method of this embodiment, the content of impurity combustible gases can be kept within the allowable range, and since they are all combustible gases and fuels, no further separation is required.

[0066] In the above embodiments, Ni / activated carbon absorbs waves. Catalytic bifunctional materials can be prepared by the following impregnation method: (1) Weigh 0.02 mol of Ni(NO3)2·6H2O and dissolve each in 30 mL of deionized water. Stir until completely dissolved to prepare metal salt impregnation solution.

[0067] (2) Weigh 10.00 g of activated carbon and add it to a nickel-containing metal salt impregnation solution. Stir continuously at room temperature for 12 h to ensure that the activated carbon carrier is in full contact with and adsorbs the metal ions.

[0068] (3) Transfer the impregnated slurry to a drying oven and dry it at 105°C for 24 h to completely remove moisture and obtain a solid powder loaded with metal precursor.

[0069] (4) The dried solid material is placed in a tube furnace and heated to 800°C at a rate of 10°C / min under nitrogen atmosphere protection (gas flow rate of 150 mL / min). The temperature is maintained at this temperature for 30 min to decompose the metal nitrate into the corresponding metal oxide or element, and finally obtain Ni / activated carbon microwave absorbing-catalyzing bifunctional material.

[0070] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0071] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0072] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0073] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0074] In this invention, the terms "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to a specific feature, structure, material, or characteristic described in connection with that embodiment or example, which is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0075] Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of the present invention.

Claims

1. A microwave-driven biomass in-situ carbon capture and hydrogen production device, characterized in that, include: A pyrolysis reactor having an inlet and an outlet, the inlet of which is used to introduce a mixture of inert gas and water vapor into the pyrolysis reactor, and the pyrolysis reactor being connected to a first microwave generator. A catalytic adsorption reactor is used to adsorb carbon dioxide from pyrolysis gas. The catalytic adsorption reactor has an inlet and an outlet. The inlet of the catalytic adsorption reactor is connected to the outlet of the pyrolysis reactor. The catalytic adsorption reactor is connected to a second microwave generator. A condenser is provided, the inlet of which is connected to the outlet of the catalytic adsorption reactor, so as to separate the tar from the hydrogen by condensation. A gas dryer, the inlet of which is connected to the outlet of the condenser, is used to remove moisture from the hydrogen gas.

2. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 1, characterized in that, The pyrolysis reactor is located above the catalytic adsorption reactor. The exhaust port of the pyrolysis reactor is connected to the inlet of the catalytic adsorption reactor via a connecting pipe. A first baffle is connected to the bottom of the pyrolysis reactor, and a second baffle is connected to the bottom of the catalytic adsorption reactor. The first baffle and the second baffle each have multiple gas passage holes for gas flow.

3. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 1, characterized in that, It also includes a gas mixer having a first inlet, a second inlet, and an outlet. The first inlet of the gas mixer is connected to an inert gas source, the second inlet of the gas mixer is connected to a steam generator, and the outlet of the gas mixer is connected to the gas inlet of the pyrolysis reactor.

4. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 3, characterized in that, The outlet of the gas mixer is connected to the inlet of the pyrolysis reactor via a heat tracing pipe. The connecting pipe is made of quartz and has a heat tracing cable attached to its exterior.

5. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 3, characterized in that, The inlet of the steam generator is connected to a liquid injection pump.

6. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 1, characterized in that, The pyrolysis reactor is connected to a first non-contact infrared thermometer, which is electrically connected to the first microwave generator. The catalytic adsorption reactor is connected to a second non-contact infrared thermometer, which is electrically connected to the second microwave generator.

7. The microwave-driven biomass in-situ carbon capture and hydrogen production device according to claim 1, characterized in that, It also includes a gas chromatography-mass spectrometry (GC-MS) instrument, which is connected to the outlet of the gas dryer to analyze the composition and concentration of the final gaseous products online.

8. A microwave-driven in-situ carbon capture and hydrogen production method for biomass, characterized in that, The microwave-driven biomass in-situ carbon capture and hydrogen production device according to any one of claims 1-7 comprises the following steps: S1. Place biomass and microwave absorber in a pyrolysis reactor, and place microwave-absorbing-catalytic bifunctional material and carbon dioxide adsorbent in a catalytic adsorption reactor; S2. Purge the pyrolysis reactor and the catalytic adsorption reactor with inert gas; S3. Inert gas and water vapor are introduced into the pyrolysis reactor and the catalytic adsorption reactor, and the first microwave generator and the second microwave generator are turned on at the same time. S4. The pyrolysis gas generated in the pyrolysis reactor enters the catalytic adsorption reactor to remove carbon dioxide from the pyrolysis gas. S5. The pyrolysis gas with carbon dioxide removed is passed into a condenser to separate the tar from the pyrolysis gas. After the tar-removed gas is dehydrated by a gas dryer, hydrogen is obtained.

9. The microwave-driven in-situ carbon capture and hydrogen production method for biomass according to claim 8, characterized in that, In step S1, the biomass and the microwave absorber are uniformly mixed and then placed in the pyrolysis reactor, with the microwave absorber accounting for 10% to 50% of the total mass of the biomass and the microwave absorber.

10. The microwave-driven in-situ carbon capture and hydrogen production method for biomass according to claim 8, characterized in that, In step S1, wave absorption The catalytic bifunctional material and carbon dioxide adsorbent are packed in a layered manner, with the microwave absorbing material being the core component. The catalytic bifunctional material is positioned above the carbon dioxide adsorbent, and the amount of carbon dioxide adsorbent added is [amount missing - likely a specific concentration]. The mass of the catalytic bifunctional material is 1 to 5 times that of the catalytic bifunctional material.

Images