A method and device for photo-thermal synergistic self-heating carbon capture and in-situ conversion

Abstract

The application discloses a kind of photo-thermal synergic self-heating carbon capture and in-situ conversion method and device, it is related to flue gas carbon dioxide capture and resource utilization technical field, wherein the method includes: the flue gas containing carbon dioxide is passed into the adsorption tower equipped with core-shell type photo-thermal adsorption catalytic particles, and carbon dioxide is adsorbed by particle core layer at normal temperature;After core layer adsorption saturation, adsorption tower is switched to closed cycle, and the light focusing system is started to focus sunlight, so that shell layer photo-thermal material generates plasmonic resonance effect and forms local high temperature, drives core layer to desorb carbon dioxide;Desorbed carbon dioxide and hydrogen occur hydrogenation reaction on the surface of shell layer catalyst, and in-situ generate liquid formic acid and release reaction heat;Relies on the heat to build self-heating cycle, auxiliary adsorbent is completely regenerated, collects tower bottom liquid formic acid, equipment is switched back to adsorption mode, and complete single-tower complete working cycle.The application realizes carbon dioxide adsorption in-situ conversion by photo-thermal coupling self-heating cycle, and reduces regeneration energy consumption.

Description

Technical Field

[0001] This invention relates to the field of flue gas carbon dioxide capture and resource utilization technology, and in particular to a photothermal synergistic self-heating carbon capture and in-situ conversion method and apparatus. Background Technology

[0002] Under the "dual carbon" goal, carbon capture, utilization, and storage (CCUS) technology is considered one of the key technological pathways to achieve low-carbon utilization of fossil energy and deep emission reduction in industrial processes. However, existing carbon capture technologies face a severe "energy consumption paradox" in the process of engineering promotion, namely, the capture process itself consumes a lot of energy, which weakens the emission reduction effect and significantly increases operating costs.

[0003] Specifically, while the mainstream amine solution absorption method (such as the monoethanolamine method) is technologically mature, its regeneration energy consumption is extremely high. After absorbing carbon dioxide from the flue gas, this process requires heating the rich solution to approximately 120°C or higher to desorb high-concentration carbon dioxide. This process typically consumes 20% to 30% of the total low-pressure steam in the power plant, directly leading to a decrease in the power plant's net efficiency of 8 to 12 percentage points. More importantly, the indirect carbon emissions from this additional energy consumption partially offset the emission reduction benefits of the capture itself, keeping capture costs persistently high and making it difficult to meet the economic requirements of large-scale industrial applications.

[0004] While solid adsorption methods (such as molecular sieves, activated carbon, and metal-organic frameworks) can avoid problems like solvent evaporation and corrosion, they still rely on external electric heating or heat transfer oil for thermal desorption and regeneration. These methods have inherent drawbacks such as high thermal inertia, slow heating rates, and a high risk of localized overheating. Furthermore, adsorption and desorption must be performed step-by-step in independent equipment or alternating modes, making continuous operation difficult. In addition, solid adsorbents are prone to structural collapse or deactivation of active sites during repeated thermal cycling, leading to decreased stability and further limiting their long-term operational reliability.

[0005] More importantly, existing technologies generally separate carbon dioxide capture and subsequent utilization into two independent stages, forming a "capture" process. compression store transportation The long-chain model of "reuse" involves multiple stages of compression, liquefaction, tank storage, and tank truck transfer, resulting in significant energy losses and capital investment. Furthermore, the high complexity of logistics reduces overall operational efficiency. In particular, the lack of an integrated system capable of directly converting high-concentration carbon dioxide in situ into high-value-added chemicals (such as formic acid and methanol precursors) within the capture tower leads to a general lack of endogenous economic drivers for carbon capture, utilization, and storage projects, making it difficult to break free from dependence on policy subsidies.

[0006] In summary, existing carbon capture technologies have significant shortcomings in terms of regeneration energy consumption, adsorbent thermal stability, and synergy between capture and utilization. There is an urgent need to develop a novel carbon capture technology capable of utilizing low-grade thermal energy, achieving self-thermal regeneration, and possessing in-situ conversion capabilities to overcome current energy efficiency and economic bottlenecks. Substantial innovations are urgently needed in areas such as photothermal synergistic catalytic materials, self-heating circulating reactor design, and solar energy-chemical thermal coupling mechanisms to drive a leapfrog development of carbon capture, utilization, and storage technologies towards low energy consumption, high efficiency, and resource utilization. Summary of the Invention

[0007] The main objective of this invention is to provide a photothermal synergistic self-heating carbon capture and in-situ conversion method.

[0008] Another objective of this invention is to provide a photothermal synergistic self-heating carbon capture and in-situ conversion device.

[0009] The third objective of this invention is to provide an electronic device.

[0010] A fourth objective of this invention is to provide a non-transitory computer-readable storage medium.

[0011] To achieve the above objectives, a first aspect of the present invention proposes a photothermal synergistic self-heating carbon capture and in-situ conversion method, comprising:

[0012] Carbon dioxide-containing flue gas is passed into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and carbon dioxide is adsorbed through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature. Once the core layer adsorption reaches saturation, the adsorption tower is switched to closed-loop circulation and the concentrating system is started. The tower body is irradiated with focused sunlight, causing the photothermal material in the shell of the core-shell type photothermal adsorption catalytic particles to generate a local surface plasma resonance effect, forming a local high temperature, which drives the core layer to desorb carbon dioxide. The desorbed carbon dioxide reacts with the introduced hydrogen gas on the surface of the catalyst in the shell layer to produce liquid formic acid in situ and release heat of reaction. The heat of reaction is used to assist the desorption of the surrounding core layer, forming a self-heating cycle that is initiated by photothermal reaction and sustained by chemical exothermic reaction until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, thus completing the self-heating regeneration, conversion and product collection cycle of a single tower.

[0013] Optionally, carbon dioxide-containing flue gas is passed into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and carbon dioxide is adsorbed through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature, including: Carbon dioxide-containing flue gas is introduced into the adsorption tower from the bottom inlet, so that the flue gas flows from bottom to top through the bed filled with core-shell type photothermal adsorption catalytic particles. Under normal temperature conditions, carbon dioxide in flue gas is selectively adsorbed by the core layer of the core-shell type photothermal adsorption catalytic particles, and carbon dioxide is enriched in the pore structure of the core layer. The concentration of carbon dioxide in the gas at the outlet of the adsorption tower is monitored in real time. When the outlet concentration reaches the preset penetration value, it is determined that the core layer adsorption has reached saturation. Then, the flue gas supply is stopped and the inlet valve and outlet valve of the tower are closed.

[0014] Optionally, the adsorption tower can be switched to closed-loop circulation and the concentrating system can be started, including: Close the flue gas inlet pipe and the purified gas outlet pipe that connect the adsorption tower to the outside world, so that the adsorption tower is physically isolated from the outside atmosphere. The light-concentrating system is activated, and sunlight is focused and directed onto the outer wall of the adsorption tower through the concentrator, so that the light energy is concentrated and projected onto the core-shell type photothermal adsorption catalytic particle bed inside the tower. Based on the preset temperature target value inside the tower, the focusing angle and focusing intensity of the condenser lens are dynamically adjusted until the local temperature inside the tower reaches a level sufficient to drive the desorption of carbon dioxide from the core layer.

[0015] Optionally, by irradiating the tower with focused sunlight, the photothermal material in the shell of the core-shell photothermal adsorption catalytic particles generates a localized surface plasmon resonance effect, forming a localized high temperature that drives the core layer to desorb carbon dioxide, including: By utilizing the photothermal material in the shell of core-shell type photothermal adsorption catalytic particles to absorb and focus sunlight, and excite the local surface plasmon resonance effect, light energy is converted into heat energy. The resonance effect generates local high temperatures in the nanoscale range of the shell layer, making the local temperature higher than the adsorption equilibrium temperature of carbon dioxide in the core layer material, thereby destroying the adsorption bond between carbon dioxide and the core layer. The localized high temperature is rapidly conducted to the core layer through the core-shell interface inside the particle, causing the adsorbed carbon dioxide molecules in the core layer to desorb and be released into the gas phase space inside the tower in a high-purity form.

[0016] Optionally, the desorbed carbon dioxide and the introduced hydrogen gas are subjected to a hydrogenation reaction on the catalyst surface of the shell layer to generate liquid formic acid in situ and release heat of reaction, including: After the desorbed carbon dioxide accumulates in the gas phase space inside the tower, hydrogen is introduced into the adsorption tower at a controlled flow rate to fully mix the hydrogen and carbon dioxide inside the tower. The mixed gas flows through the surface of the shell of the core-shell photothermal adsorption catalytic particles, where carbon dioxide hydrogenation occurs at the active sites of the catalyst contained in the shell, generating liquid formic acid in situ. The reaction temperature and pressure are controlled so that the generated formic acid condenses in liquid form and deposits at the bottom of the tower, while the hydrogenation reaction releases additional heat of reaction.

[0017] Optionally, the heat of reaction is used to assist the desorption of the surrounding core layer, forming a self-heating cycle that is initiated by photothermal reaction and sustained by chemical exothermic reaction, until the adsorbent is completely regenerated, including: The heat of reaction released on the surface of the shell catalyst during the hydrogenation reaction is collected and transferred to the peripheral core region that has not yet been desorbed or is in the process of desorption through convective heat transfer in the gas phase inside the tower and solid-phase heat conduction between particles. The heat of reaction is used to raise the local temperature of the surrounding core layer, which further desorbs the residual carbon dioxide in the core layer of this region, reducing the need for continuous energy supply from the external concentrating system. When the carbon dioxide desorbed from the surrounding core layer continues to participate in the hydrogenation reaction and release more heat of reaction, a self-heating cycle is formed, which is initiated by photothermal reaction and maintained by chemical exothermic reaction, until the core layer adsorbent of the entire bed is completely regenerated.

[0018] Optionally, after the generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank, the system switches back to adsorption mode, including: When the amount or concentration of liquid formic acid accumulated at the bottom of the tower reaches the preset discharge conditions, the product collection valve located at the bottom of the tower is opened, and the liquid formic acid is transported to an external storage tank while maintaining the closed-loop circulation pressure inside the adsorption tower. Close the product collection valve and simultaneously replenish the column with fresh hydrogen to maintain the reactant concentration for the hydrogenation reaction in subsequent cycles; After confirming that the core layer adsorbent has been completely regenerated and all liquid formic acid has been discharged, stop the irradiation of the focusing system and open the flue gas inlet and purified gas outlet to restore the flow of normal temperature flue gas, so that the adsorption tower can resume adsorption mode.

[0019] To achieve the above objectives, a second aspect of the present invention provides a photothermal synergistic self-heating carbon capture and in-situ conversion device, comprising: An adsorption module is used to pass carbon dioxide-containing flue gas into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and adsorb carbon dioxide through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature. The desorption module is used to switch the adsorption tower to closed-loop circulation and start the concentrating system when the core layer adsorption reaches saturation. The focused sunlight is used to irradiate the tower body, so that the photothermal material in the shell layer of the core-shell type photothermal adsorption catalytic particles generates a local surface plasma resonance effect, forming a local high temperature, which drives the core layer to desorb carbon dioxide. The conversion module is used to perform a hydrogenation reaction between the desorbed carbon dioxide and the introduced hydrogen gas on the catalyst surface of the shell layer, generating liquid formic acid in situ and releasing heat of reaction. The regeneration module is used to assist the desorption of the surrounding core layer by utilizing the heat of reaction, forming a self-heating cycle that is initiated by photothermal reaction and maintained by chemical exothermic reaction until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, thus completing the self-heating regeneration, conversion and product collection cycle of a single tower.

[0020] Regarding the apparatus in the above embodiments, the specific manner in which each module performs its operation has been described in detail in the embodiments related to the method, and will not be elaborated upon here.

[0021] To achieve the above objectives, a third aspect of this application provides an electronic device, including a processor and a memory; wherein the processor reads executable program code stored in the memory to run a program corresponding to the executable program code, for implementing a photothermal synergistic self-heating carbon capture and in-situ conversion method as described in the first aspect embodiment.

[0022] To achieve the above objectives, a fourth aspect of this application provides a non-transitory computer-readable storage medium storing a computer program thereon, which, when executed by a processor, implements a photothermal synergistic self-heating carbon capture and in-situ conversion method as described in the first aspect embodiment.

[0023] The embodiments of the present invention have the following beneficial effects: 1. Significantly reduced regeneration energy consumption. Utilizing the localized surface plasmon resonance effect of shell-plasma gold nanoparticles, local high temperatures are instantaneously generated at the nanoscale under focused sunlight irradiation, achieving rapid desorption within minutes. This avoids the dependence on large amounts of low-pressure steam in the traditional amine method, significantly reducing parasitic energy consumption in the carbon capture process.

[0024] 2. Construct a self-heating energy complementarity mechanism. The chemical heat released by the hydrogenation reaction is actively collected and used to assist in the desorption of surrounding core layers, forming a "photothermal start-up". The self-heating cycle of "chemical exothermic maintenance" reduces the dependence on continuous external light and improves the system's operational stability under different weather conditions.

[0025] 3. Achieve integrated capture and in-situ conversion. The desorbed high-purity carbon dioxide does not need to go through intermediate steps such as compression, storage, and transportation. It directly reacts with hydrogen on the surface of the catalyst in the inner shell of the tower to generate liquid formic acid, shortening the process chain and avoiding energy loss and investment costs in intermediate steps.

[0026] 4. Enhance system economics and product added value. The product is liquid formic acid, which is easy to store and transport and has clear market application value. This transforms the carbon capture process from simple environmental governance to resource utilization, thereby enhancing the endogenous economic driving force of carbon capture, utilization and storage projects.

[0027] 5. Expanding the utilization pathways of low-grade solar energy. By converting intermittent, low-energy-density sunlight into high-energy-density localized high temperatures through plasma photothermal effects, and coupling this with exothermic chemical reactions, a novel approach is provided for the efficient utilization of low-grade thermal energy in the field of carbon capture. Attached Figure Description

[0028] 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, wherein: Figure 1 A flowchart of a photothermal synergistic self-heating carbon capture and in-situ conversion method provided in an embodiment of the present invention; Figure 2 This is a structural diagram of a photothermal synergistic self-heating carbon capture and in-situ conversion device provided in an embodiment of the present invention. Detailed Implementation

[0029] It should be noted that, unless otherwise specified, the embodiments and features described in the present invention can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0030] To enable those skilled in the art to better understand the present invention, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort should fall within the scope of protection of the present invention.

[0031] The following description, with reference to the accompanying drawings, describes a method and apparatus for photothermal synergistic self-heating carbon capture and in-situ conversion according to an embodiment of the present invention.

[0032] Example 1 This invention provides a photothermal synergistic self-heating carbon capture and in-situ conversion method. Figure 1 This is a schematic flowchart of a photothermal synergistic self-heating carbon capture and in-situ conversion method provided in an embodiment of the present invention. Figure 1 As shown, the method includes the following steps: Step S1: Pass the flue gas containing carbon dioxide into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and adsorb carbon dioxide through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature.

[0033] The entire adsorption conversion tower adopts a double-layer jacket design. Based on the jacket separation, different functional areas are spatially divided. The internal space of the tower is divided into two functional zones. The inner cavity of the jacket forms the reaction zone where flue gas contacts the packing, while the outer cavity of the jacket serves as the photothermal heat collection zone for receiving the concentrated light source. The two cavities are separated from each other but share the tower enclosure structure, which can not only isolate unnecessary heat crosstalk between areas but also complete heat conduction through the tower wall. The entire space inside the reaction zone is uniformly filled with customized core-shell photothermal adsorption catalytic particles. The particles are processed and shaped according to a uniform ratio. The particles are divided into inner and outer layers. The inner core layer is made of modified metal-organic framework materials, namely MOFs. The modification treatment can optimize the pore size distribution and surface polarity of the material, and improve the targeted adsorption capacity of carbon dioxide. The outer shell layer is a nanocomposite material that completely covers the core. It is prepared by combining plasma gold nanoparticles (Au NPs) and copper-based catalytic components according to a predetermined ratio. The dense coating structure of the shell layer can protect the inner adsorption core layer and ensure that the light energy can fully contact the photothermal active components.

[0034] When carrying out the adsorption operation in this stage based on the above tower body and packing structure, the industrial flue gas containing carbon dioxide is sent into the reaction zone inside the tower through a dedicated feed pipeline at the bottom of the adsorption conversion tower. The feed pipeline is equipped with a flow-limiting valve to stabilize the inlet flow rate. The flue gas relies on its own pressure difference to pass through the internal packing bed at a uniform speed from bottom to top. The airflow is evenly dispersed in the gaps between the bed layers, increasing the effective contact area between the flue gas and the particulate packing. The environment inside the tower is maintained at normal temperature throughout the process. At this time, the concentrated photovoltaic system matched with the outer layer of the tower is in a shut-off state, and no external light energy is input to the photothermal heat collection area, avoiding excess heat that would cause a decrease in the adsorption capacity of the adsorption material.

[0035] During this stage of room-temperature adsorption, the adsorption capacity of MOFs for carbon dioxide can be characterized by the following calculation formula:

[0036] in, Represents the equilibrium adsorption capacity of the modified MOF material, in mg / g; This represents the Freundrich adsorption constant for the corresponding modified MOF material; This represents the equilibrium concentration of carbon dioxide in the gas phase within the column, expressed in mg / L. This represents the adsorption characteristic constant, which is related to the strength of the interaction between the adsorbent and the adsorbate.

[0037] As the flue gas flows upward, the carbon dioxide component in the gas flow comes into full contact with the modified MOFs material in the core layer of the packing. The well-developed pore structure of the modified MOFs can selectively adsorb carbon dioxide. The carbon dioxide molecules are bound inside the pores by the intermolecular van der Waals forces. The carbon dioxide molecules are fixed and enriched in the pores inside the MOFs. Other exhaust gas components that are difficult to be adsorbed are not intercepted. The clean flue gas after removing carbon dioxide continues to move upward and is finally discharged from the gas outlet pipe at the top of the adsorption tower.

[0038] Throughout the continuous flue gas flow, gas component sensors installed at the outlet of the tower continuously collect carbon dioxide concentration data of the outlet flue gas in real time. The collected concentration data is transmitted back to the supporting intelligent control system in real time. The system determines the adsorption saturation state based on the pre-entered and process test-calibrated carbon dioxide penetration critical threshold. Once the sensor's actual monitoring data reaches the set threshold, it means that the effective adsorption sites of the packing bed are approaching saturation. The system immediately issues an automatic command to shut down the flue gas inlet valve and the purified gas outlet valve, quickly cutting off the connection between the tower and the external flue gas pipeline and tail gas emission pipeline, terminating the flue gas feeding process, marking the formal end of the single ambient temperature adsorption process in this embodiment of the application. The tower then has the basic conditions to enter the subsequent closed desorption process.

[0039] Step S2: When the core layer adsorption reaches saturation, the adsorption tower is switched to closed-loop circulation and the focusing system is started. The tower body is irradiated with focused sunlight, which causes the photothermal material in the shell of the core-shell type photothermal adsorption catalytic particles to generate a local surface plasma resonance effect, forming a local high temperature, and driving the core layer to desorb carbon dioxide.

[0040] After completing the S1 adsorption saturation determination and shutting off the inlet and outlet valves, the adsorption tower immediately enters a closed-loop control state. The valve actuators act quickly under the command of the control system, sealing off all pipelines connecting the tower to the outside atmosphere. From the flue gas feed pipeline and the purified gas discharge pipeline to all kinds of auxiliary pressure measurement bypasses, all are completely sealed off, forming a closed-loop circulation cavity in the reaction zone inside the tower that is completely isolated from the external environment. This not only prevents the high-purity carbon dioxide gas components enriched in the tower from leaking outward and causing raw material loss, but also prevents outside air from seeping back into the tower to dilute the concentration of gaseous carbon dioxide and introduce impurities that may interfere with subsequent catalytic conversion reactions.

[0041] After the sealed operation is completed, the matching concentrated photovoltaic module is started. This module is equipped with multiple sets of adjustable angle concentrators. Each set of concentrators is independently equipped with a small servo adjustment component. Relying on the optical converging effect of the concentrators, natural sunlight is directionally focused and projected onto the outer photothermal heat collection area of ​​the tower. The converged light energy is gradually conducted along the interlayer space of the double-layer jacket and transferred to the packing bed inside the tower through the heat exchange surface of the tower wall, ensuring that the light energy can stably act on the core-shell catalytic adsorption particles packed inside the bed.

[0042] The intelligent control system of this application connects to temperature and pressure sensing elements deployed inside the tower. Various sensors are evenly distributed in the upper and middle sections of the packing bed and in the gas phase cavity inside the tower. The sensors continuously collect real-time temperature and cavity pressure parameters inside the tower, and the collected data is transmitted back to the control terminal in real time. Based on the collected data and the pre-entered desorption temperature target parameters, the control system automatically fine-tunes the pitch angle and opening and closing amplitude of the focusing mirror, thereby changing the focusing intensity and flexibly controlling the total amount of light energy entering the tower. This avoids the problem of packing overheating and loss caused by excessive local focusing, and prevents abnormal high temperature from causing Au NPs agglomeration and deactivation in the shell or MOF skeleton to collapse due to heat.

[0043] The focused light energy is efficiently captured by Au NPs plasmonic particles inside the shell. The gold nanoparticles excited by the light energy generate a localized surface plasmonic resonance effect. This physical effect enables the rapid conversion of light energy into heat energy in the nanoscale shell region. The relevant energy conversion relationship can be characterized by the following formula:

[0044] in, This represents the localized thermal energy generated by Au NPs through plasma resonance, expressed in J. The light-to-thermal energy conversion efficiency of gold nanoparticles; The intensity of solar radiation incident on the surface of the filler after concentration, expressed in units of... ; The effective surface area of ​​the filler particles exposed to light, per unit. .

[0045] Based on the above-mentioned thermal energy generation process, the local ambient temperature of the shell can exceed 150℃. The adsorption equilibrium temperature of carbon dioxide for the modified MOFs material can be explained with the help of the equilibrium temperature calculation formula:

[0046] in, The equilibrium temperature for carbon dioxide adsorption by MOFs, in °C; The adsorption temperature is based on atmospheric pressure and is expressed in °C. The temperature correlation coefficient for carbon dioxide partial pressure; This represents the partial pressure of carbon dioxide in the gas phase inside the tower, expressed in Pa.

[0047] The generated local high temperature is much higher than the adsorption equilibrium temperature of carbon dioxide in the modified MOF core layer. The high temperature is rapidly conducted inward to the MOF core layer through the contact interface where the two materials of the core and shell are closely bonded. From a thermodynamic point of view, it destroys the adsorption binding force between carbon dioxide molecules and MOF pores formed by van der Waals forces. The carbon dioxide that was originally adsorbed and fixed inside the core layer pores undergoes desorption. High-purity carbon dioxide gas is released from the inside of the packing and accumulates in the closed gas phase space inside the tower. The entire desorption process can be completed within minutes, which greatly shortens the adsorbent regeneration time and reserves sufficient reaction time for the subsequent in-situ hydrogenation of carbon dioxide to produce formic acid.

[0048] In step S3, the desorbed carbon dioxide and the introduced hydrogen gas are subjected to a hydrogenation reaction on the catalyst surface of the shell layer to generate liquid formic acid in situ and release heat of reaction.

[0049] As the desorption process continues, high-purity carbon dioxide released from the core layer of the core-shell photothermal adsorption catalytic particles is continuously precipitated and accumulates in the closed gas phase space within the tower, gradually increasing the carbon dioxide gas concentration and providing sufficient reactants for the subsequent catalytic hydrogenation reaction. In the actual process operation of this embodiment, the system continuously introduces high-purity hydrogen into the completely closed-loop tower cavity through a dedicated hydrogen feed pipeline pre-programmed into the tower body, adhering strictly to a constant flow rate. After entering the closed cavity, the hydrogen rapidly mixes and fuses with the carbon dioxide gas released from the previous photothermal desorption, relying on the thermal disturbance and airflow diffusion of the existing gas within the tower. This ultimately forms a uniformly composed and stably concentrated binary mixture of carbon dioxide and hydrogen in the reaction zone within the tower, effectively avoiding incomplete reactions caused by localized enrichment of a single component or uneven gas mixing.

[0050] Driven by a slight pressure difference within the column, the mixed reactant gas maintains a stable flow rate through the packed bed, ensuring full contact with the copper-based catalyst shell layer surrounding the core-shell particles. The carbon dioxide and hydrogen components in the mixed gas precisely adhere to the active sites on the surface of the copper-based catalyst, subsequently undergoing a highly efficient carbon dioxide hydrogenation catalytic reaction. The corresponding core chemical reaction formula is: This means that carbon dioxide and hydrogen undergo a combination reaction under catalytic conditions to generate the target product, formic acid, in situ.

[0051] Throughout the entire hydrogenation reaction process, the intelligent control system implemented in this application monitors and precisely controls two key operating parameters within the tower: reaction temperature and chamber pressure. By dynamically fine-tuning these parameters, the system precisely regulates the formation phase of formic acid. Utilizing a stable and controllable temperature and pressure environment within the tower, the gaseous formic acid product rapidly reaches the phase transition conditions, condensing from a gaseous state to a liquid state. The liquid product then continues to settle downwards under its own gravity, eventually accumulating stably in the designated collection area at the bottom of the adsorption tower, completing the initial enrichment and collection of the product.

[0052] Meanwhile, the chemical reaction for the hydrogenation of carbon dioxide to formic acid is essentially an exothermic reaction. Throughout the entire forward reaction, a large amount of heat is continuously released. This heat is distinct from the externally generated photothermal energy from the earlier Au NPs photothermal conversion; it is an endogenous heat generated within the system and is the core heat source for constructing the subsequent self-heating cycle. The total heat released by this hydrogenation reaction can be accurately calculated using the reaction heat release metric formula:

[0053] in, The total heat of chemical reaction released during the entire hydrogenation reaction is represented by J. This represents the amount of carbon dioxide that actually participates in the hydrogenation reaction during the current reaction period, expressed in mol. This is the constant enthalpy change of a unit mole of carbon dioxide hydrogenated in situ to form formic acid under standard operating conditions, expressed in J / mol. This parameter is determined by the thermodynamic properties of the reaction itself and is a fixed process parameter.

[0054] Based on this, the reaction progress formula can be used to further characterize the degree of reaction and accurately match the heat generation and raw material consumption patterns:

[0055] in, Represents the conversion rate of carbon dioxide hydrogenation reaction, dimensionless; This represents the amount of carbon dioxide that has participated in the reaction, expressed in mol. This represents the total amount of carbon dioxide initially involved in the mixing within the tower, expressed in mol.

[0056] By monitoring the reaction conversion rate in real time, the reaction exothermic rate and total exothermic amount can be accurately predicted, providing data support for the stable operation of the system's self-heating cycle.

[0057] Step S4 utilizes the heat of reaction to assist the desorption of the surrounding core layer, forming a self-heating cycle of photothermal initiation and chemical exothermic maintenance until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, completing the self-heating regeneration, conversion and product collection cycle of a single tower.

[0058] The endogenous chemical reaction heat generated by the hydrogenation reaction is mainly transferred within the tower via two pathways: convective heat transfer and solid-phase heat conduction. In the closed tower cavity environment of this embodiment, heat first diffuses rapidly and uniformly within the cavity through convective heat transfer of the sealed mixed gas, causing the overall ambient temperature within the tower to steadily increase. Simultaneously, heat is efficiently transferred to the surrounding MOF core layer region, which has not yet completed desorption, via the solid-phase contact surface of adjacent core-shell photothermal adsorption catalytic particles through solid-phase heat conduction.

[0059] To quantify the heat transfer efficiency of this process, it can be characterized by the comprehensive heat transfer formula within the tower:

[0060] in, The total heat transfer within the tower per unit time, expressed in J / s; This refers to the heat transfer caused by gas convection, expressed in J / s. The solid phase heat conduction of the filler particles is expressed in J / s.

[0061] Under the continuous heating effect of the residual heat from the reaction, the temperature of the partially desorbed MOF core layer in the surrounding area continues to rise, effectively disrupting the adsorption equilibrium between residual carbon dioxide and the pore structure of the MOFs. This promotes further desorption and precipitation of the residual adsorbed carbon dioxide inside the core layer. The newly generated carbon dioxide gas immediately replenishes the sealed gas phase space inside the tower, continuously participating in the hydrogenation catalytic reaction on the surface of the copper-based catalyst in the shell layer, and continuously releasing new chemical reaction heat. This forms a virtuous cycle, establishing a complete self-heating operation system. The entire system relies on external solar heat for initial heating and startup, and subsequently relies on the internal heat released by the chemical reaction to maintain heating, without the need for continuous external energy consumption. During the uninterrupted and stable operation of the entire self-heating cycle, the packed bed inside the tower follows the desorption law from local areas to the entire bed, gradually completing the carbon dioxide desorption operation until all the MOFs adsorbed core layers inside the tower are completely desorbed, achieving complete regeneration of the adsorbent.

[0062] In this embodiment, a dedicated in-situ product collection module is installed at the bottom of the tower to provide hardware support for the real-time detection, automatic discharge, and storage of formic acid products. This module integrates a high-precision online formic acid concentration detection element and an electronically controlled product collection valve. During operation, the intelligent control system continuously collects and monitors the volume and concentration parameters of the liquid formic acid accumulated at the bottom of the tower in real time, constantly comparing the measured data with the system's preset product discharge threshold. When any or both parameters of formic acid concentration and accumulation volume reach the preset threshold, the control system prioritizes pressure stabilization and regulation. Under the premise of maintaining stable pressure in the closed-loop circulation chamber within the tower and ensuring stable reaction conditions within the tower, it automatically triggers a command to open the bottom product collection valve, allowing the high-purity liquid formic acid accumulated at the bottom of the tower to be smoothly transported to an external finished product storage tank via a dedicated discharge pipeline, completing the sealed storage of the product and effectively preventing product volatilization and loss.

[0063] After a single formic acid discharge process is completed, the system automatically closes the product collection valve, cutting off the connection between the tower and the storage tank. Simultaneously, the hydrogen supply pipeline is activated to precisely replenish fresh, high-purity hydrogen into the tower cavity, ensuring real-time replenishment of the hydrogen reactant raw materials consumed during the hydrogenation reaction. This guarantees a stable concentration of reactant components within the tower, providing sufficient material reserves for the next round of catalytic reaction and ensuring the continuity and stability of the entire cycle process.

[0064] Once the system sensors confirm that the adsorption packing inside the tower has been completely regenerated and the liquid formic acid enriched at the bottom of the tower has been completely transported to the storage tank, the intelligent control system issues a shutdown and reset command, shutting down the external photovoltaic concentrator system, completely terminating the solar focusing irradiation operation, and ceasing the input of external light and heat into the tower. Subsequently, the system gradually reopens the flue gas inlet valve at the bottom of the tower and the purified gas outlet valve at the top of the tower, smoothly restoring the tower from a closed-loop operation to a circulating condition connected to the outside. As external heating ceases and the tower is ventilated and heat exchanged, the ambient temperature inside the tower gradually drops to room temperature. The adsorption conversion tower officially completes the entire process of photothermal regeneration, catalytic conversion, and product collection, and switches back to the room temperature flue gas adsorption operating mode corresponding to S1. Thus, the single tower completes the complete closed-loop cycle of adsorption enrichment, photothermal regeneration, in-situ catalytic conversion, and product collection.

[0065] In the practical engineering application of this application embodiment, to address the technical shortcomings of single-tower equipment being unable to continuously process industrial flue gas and experiencing intermittent operating conditions, the entire process unit adopts a multi-stage adsorption conversion tower group parallel layout structure. This scheme preferably uses a three-tower coordinated operation process route. The three adsorption conversion towers, with completely identical structures and performance, adopt a staggered and alternating operation mode. The equipment is arranged in an orderly sequence during operation. At any given time, one adsorption tower performs the S1 ambient temperature flue gas adsorption and enrichment process, responsible for capturing and purifying carbon dioxide in the flue gas; the second adsorption tower performs the S2 to S4 photothermal regeneration, carbon dioxide catalytic conversion, and product collection processes, completing adsorbent regeneration and formic acid preparation; the remaining adsorption tower is dedicated to bed purging pretreatment operations, preparing for the next round of adsorption. Through the alternating operation of the three towers, the uninterrupted and continuous treatment of industrial flue gas by the entire unit is completely achieved, significantly improving the overall system efficiency.

[0066] The entire process is controlled and managed by an intelligent control system. In addition to the initial adaptive adjustment of the focusing angle and automatic product discharge control, the system relies on temperature and pressure sensors evenly distributed throughout the tower to collect and feedback various operational data in real time. Based on this real-time data, it dynamically and adaptively adjusts the focusing intensity and irradiation range of the concentrating photovoltaic modules. Through precise intelligent control, the problem of excessively high local temperatures within the tower is effectively avoided, preventing the copper-based catalyst from sintering and active site deactivation caused by high temperatures. This comprehensively improves the operational stability, safety, and service life of the entire photothermal synergistic carbon dioxide adsorption-conversion process.

[0067] In the application of one embodiment of the present invention, the implementation process is as follows: This application is implemented in conjunction with a real industrial park boiler flue gas treatment project. The object of treatment in this embodiment is industrial flue gas emitted from boilers in industrial parks. The system is designed with a rated flue gas treatment flow rate of 10,000 Nm³ / h, the internal carbon dioxide volume concentration of the flue gas is stably maintained at 12%, and the flue gas temperature is at normal temperature and pressure, which is suitable for the operating conditions of the photothermal synergistic adsorption conversion process of this application.

[0068] During the system's formal operation, the carbon dioxide-containing flue gas generated by the boiler is first smoothly introduced into the first-stage adsorption tower. The core-shell type photothermal adsorption catalytic particles packed within the tower complete the carbon dioxide capture operation. Under normal temperature and pressure conditions, the modified MOFs material in the core layer of the packing, with its porous structure and selective adsorption characteristics, stably captures the carbon dioxide component in the flue gas, achieving efficient enrichment of carbon dioxide. The purified flue gas, after carbon dioxide removal, directly meets emission standards and is stably discharged from the top of the adsorption tower, completing the flue gas purification treatment. The adsorption load in this stage can be characterized by the formula for the carbon dioxide adsorption capacity of the flue gas:

[0069] wherein, is the single-hour carbon dioxide treatment capacity of flue gas, with the unit of kg / h; is the flue gas flow rate under standard working conditions, with the unit of Nm³ / h; is the volume concentration of carbon dioxide in flue gas, which is dimensionless.

[0070] During the continuous adsorption operation of the first-stage adsorption tower, as the internal adsorption sites of the MOFs material are gradually occupied by carbon dioxide molecules, the adsorption saturation of the packed bed continuously increases, the penetration resistance of the bed gradually increases, and the pressure difference between the front and rear ends of the tower body increases synchronously with the adsorption saturation degree. In this embodiment, the pressure difference sensor matched with the tower body is used to monitor the change of bed pressure difference in real time. When the pressure difference reaches the preset alarm threshold of the system, it is determined that the MOFs adsorption particles inside the first-stage adsorption tower are completely adsorption-saturated and no longer have the capacity of efficient carbon dioxide capture. At this time, the entire control system automatically triggers a pipeline reversing command, quickly switches the flow direction of flue gas, switches the feed path of boiler flue gas to the second-stage adsorption tower, and the second-stage adsorption tower continues to undertake the flue gas adsorption and purification operation, so as to ensure the uninterrupted continuous operation of the entire flue gas treatment system.

[0071] After completing the switching of flue gas flow direction, the first-stage adsorption tower immediately closes all connecting valves at the flue gas inlet and purified gas outlet, cuts off the path connected to the external flue gas system, and the tower body enters a completely airtight isolation state. Then the system automatically starts the solar light concentrating system matched with the tower body, converges natural sunlight through an angle-adjustable condenser, and directionally irradiates the outer photothermal heat collecting area of the double-layer jacket of the adsorption tower. Light energy continuously transfers heat to the packed bed in the tower through photothermal conversion. Under the action of the Au NPs plasma photothermal effect, the local temperature of the packing in the tower rises rapidly and is stably maintained at 160°C. This temperature is higher than the carbon dioxide desorption equilibrium temperature of the MOFs material, and can fully meet the temperature requirements for the desorption and regeneration of the adsorbent.

[0072] Under the constant temperature condition of 160°C, the gold-copper composite Au / Cu catalyst in the core-shell particle shell layer of the first-stage adsorption tower gives full play to the synergistic effect of photothermal catalysis. The high-purity carbon dioxide previously adsorbed and enriched by the MOFs core layer is completely desorbed by heating, the desorbed high-purity carbon dioxide is fully mixed with hydrogen introduced at a preset flow rate into the tower, and an in-situ hydrogenation catalytic reaction occurs on the active surface of the Au / Cu catalyst to continuously form formic acid vapor.

[0073] The gaseous formic acid vapor generated in the tower settles to the bottom area of the tower along with the air flow in the tower, and undergoes heat exchange and cooling through a condensing device matched with the tower bottom. The high-temperature formic acid vapor undergoes phase change when cooled, condenses from gaseous state into high-purity liquid formic acid, and finally collects in the product storage tank at the tower bottom, completing the closed-loop collection of the product.

[0074] In this embodiment, the photothermal desorption and catalytic regeneration process runs stably for 20 minutes. This sufficient reaction time ensures that all MOF adsorption beds inside the first-stage adsorption tower completely desorb carbon dioxide, achieving complete regeneration of the adsorbent, eliminating adsorption residues, and restoring the initial adsorption capacity of the MOF materials. After the 20-minute regeneration and conversion process is completed, the system shuts down the concentrated irradiation system, stops the external photothermal input, and the tower temperature gradually and naturally drops back to room temperature. The system resets all valve states, switches the regenerated first-stage adsorption tower back to room temperature adsorption mode, and awaits the next round of adsorption, completing the single-tower adsorption, saturation switching, photothermal regeneration, and product collection and recycling process.

[0075] Example 2 This invention provides a photothermal synergistic self-heating carbon capture and in-situ conversion device. Figure 2 This is a schematic diagram of a photothermal synergistic self-heating carbon capture and in-situ conversion device provided in an embodiment of the present invention. Figure 2 As shown, the device includes: The adsorption module 100 is used to pass carbon dioxide-containing flue gas into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and adsorb carbon dioxide through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature. The desorption module 200 is used to switch the adsorption tower to closed-loop circulation and start the concentrating system when the core layer adsorption reaches saturation. The concentrated sunlight is used to irradiate the tower body, so that the photothermal material in the shell layer of the core-shell type photothermal adsorption catalytic particles generates a local surface plasma resonance effect, forming a local high temperature, which drives the core layer to desorb carbon dioxide. The conversion module 300 is used to perform a hydrogenation reaction between the desorbed carbon dioxide and the introduced hydrogen gas on the catalyst surface of the shell layer, generating liquid formic acid in situ and releasing heat of reaction. The regeneration module 400 is used to assist the desorption of the surrounding core layer by utilizing the heat of reaction, forming a self-heating cycle that is initiated by photothermal reaction and maintained by chemical exothermic reaction until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to the adsorption mode, thus completing the self-heating regeneration, conversion and product collection cycle of a single tower.

[0076] Regarding the apparatus in the above embodiments, the specific manner in which each module performs its operation has been described in detail in the embodiments related to the method, and will not be elaborated upon here.

[0077] Example 3 To implement the methods of the above embodiments, the present invention also provides an electronic device, which includes a memory and a processor; wherein the processor reads executable program code stored in the memory to run a program corresponding to the executable program code, so as to implement the various steps of the methods described above.

[0078] Example 4 To implement the above embodiments, this application also proposes a non-transitory computer-readable storage medium storing a computer program thereon, which, when executed by a processor, implements the method described in the foregoing embodiments.

[0079] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

[0080] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present 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.

[0081] 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.

Claims

1. A photothermal synergistic self-heating carbon capture and in-situ conversion method, characterized in that, include: Carbon dioxide-containing flue gas is passed into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and carbon dioxide is adsorbed through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature. Once the core layer adsorption reaches saturation, the adsorption tower is switched to closed-loop circulation and the concentrating system is started. The tower body is irradiated with focused sunlight, causing the photothermal material in the shell of the core-shell type photothermal adsorption catalytic particles to generate a local surface plasma resonance effect, forming a local high temperature, which drives the core layer to desorb carbon dioxide. The desorbed carbon dioxide reacts with the introduced hydrogen gas on the surface of the catalyst in the shell layer to produce liquid formic acid in situ and release heat of reaction. The heat of reaction is used to assist the desorption of the surrounding core layer, forming a self-heating cycle that is initiated by photothermal reaction and sustained by chemical exothermic reaction until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, thus completing the self-heating regeneration, conversion and product collection cycle of a single tower.

2. The method according to claim 1, characterized in that, Carbon dioxide-containing flue gas is passed into an adsorption tower filled with core-shell photothermal adsorption catalytic particles. At room temperature, carbon dioxide is adsorbed through the core layer of the core-shell photothermal adsorption catalytic particles, comprising: Carbon dioxide-containing flue gas is introduced into the adsorption tower from the bottom inlet, so that the flue gas flows from bottom to top through the bed filled with core-shell type photothermal adsorption catalytic particles. Under normal temperature conditions, carbon dioxide in flue gas is selectively adsorbed by the core layer of the core-shell type photothermal adsorption catalytic particles, and carbon dioxide is enriched in the pore structure of the core layer. The concentration of carbon dioxide in the gas at the outlet of the adsorption tower is monitored in real time. When the outlet concentration reaches the preset penetration value, it is determined that the core layer adsorption has reached saturation. Then, the flue gas supply is stopped and the inlet valve and outlet valve of the tower are closed.

3. The method according to claim 2, characterized in that, Switching the adsorption tower to a closed-loop circulation and starting the concentrating system includes: Close the flue gas inlet pipe and the purified gas outlet pipe that connect the adsorption tower to the outside world, so that the adsorption tower is physically isolated from the outside atmosphere. The light-concentrating system is activated, and sunlight is focused and directed onto the outer wall of the adsorption tower through the concentrator, so that the light energy is concentrated and projected onto the core-shell type photothermal adsorption catalytic particle bed inside the tower. Based on the preset temperature target value inside the tower, the focusing angle and focusing intensity of the condenser lens are dynamically adjusted until the local temperature inside the tower reaches a level sufficient to drive the desorption of carbon dioxide from the core layer.

4. The method according to claim 3, characterized in that, By irradiating the tower with focused sunlight, the photothermal material in the shell layer of the core-shell photothermal adsorption catalytic particles generates a localized surface plasmon resonance effect, forming a localized high temperature that drives the desorption of carbon dioxide from the core layer, including: By utilizing the photothermal material in the shell of core-shell type photothermal adsorption catalytic particles to absorb and focus sunlight, and excite the local surface plasmon resonance effect, light energy is converted into heat energy. The resonance effect generates local high temperatures in the nanoscale range of the shell layer, making the local temperature higher than the adsorption equilibrium temperature of carbon dioxide in the core layer material, thereby destroying the adsorption bond between carbon dioxide and the core layer. The localized high temperature is rapidly conducted to the core layer through the core-shell interface inside the particle, causing the adsorbed carbon dioxide molecules in the core layer to desorb and be released into the gas phase space inside the tower in a high-purity form.

5. The method according to claim 4, characterized in that, The desorbed carbon dioxide reacts with the introduced hydrogen gas on the catalyst surface of the shell layer to produce liquid formic acid in situ, releasing heat of reaction, including: After the desorbed carbon dioxide accumulates in the gas phase space inside the tower, hydrogen is introduced into the adsorption tower at a controlled flow rate to fully mix the hydrogen and carbon dioxide inside the tower. The mixed gas flows through the surface of the shell of the core-shell photothermal adsorption catalytic particles, where carbon dioxide hydrogenation occurs at the active sites of the catalyst contained in the shell, generating liquid formic acid in situ. The reaction temperature and pressure are controlled so that the generated formic acid condenses in liquid form and deposits at the bottom of the tower, while the hydrogenation reaction releases additional heat of reaction.

6. The method according to claim 5, characterized in that, The desorption of the surrounding core layer is assisted by the heat of reaction, forming a self-heating cycle initiated by photothermal reaction and sustained by chemical exothermic reaction, until the adsorbent is completely regenerated, including: The heat of reaction released on the surface of the shell catalyst during the hydrogenation reaction is collected and transferred to the peripheral core region that has not yet been desorbed or is in the process of desorption through convective heat transfer in the gas phase inside the tower and solid-phase heat conduction between particles. The heat of reaction is used to raise the local temperature of the surrounding core layer, which further desorbs the residual carbon dioxide in the core layer of this region, reducing the need for continuous energy supply from the external concentrating system. When the carbon dioxide desorbed from the surrounding core layer continues to participate in the hydrogenation reaction and release more heat of reaction, a self-heating cycle is formed, which is initiated by photothermal reaction and maintained by chemical exothermic reaction, until the core layer adsorbent of the entire bed is completely regenerated.

7. The method according to claim 6, characterized in that, The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, including: When the amount or concentration of liquid formic acid accumulated at the bottom of the tower reaches the preset discharge conditions, the product collection valve located at the bottom of the tower is opened, and the liquid formic acid is transported to an external storage tank while maintaining the closed-loop circulation pressure inside the adsorption tower. Close the product collection valve and simultaneously replenish the column with fresh hydrogen to maintain the reactant concentration for the hydrogenation reaction in subsequent cycles; After confirming that the core layer adsorbent has been completely regenerated and all liquid formic acid has been discharged, stop the irradiation of the focusing system and open the flue gas inlet and purified gas outlet to restore the flow of normal temperature flue gas, so that the adsorption tower can resume adsorption mode.

8. A photothermal synergistic self-heating carbon capture and in-situ conversion device, characterized in that, include: An adsorption module is used to pass carbon dioxide-containing flue gas into an adsorption tower filled with core-shell photothermal adsorption catalytic particles, and adsorb carbon dioxide through the core layer of the core-shell photothermal adsorption catalytic particles at room temperature. The desorption module is used to switch the adsorption tower to closed-loop circulation and start the concentrating system when the core layer adsorption reaches saturation. The focused sunlight is used to irradiate the tower body, so that the photothermal material in the shell layer of the core-shell type photothermal adsorption catalytic particles generates a local surface plasma resonance effect, forming a local high temperature, which drives the core layer to desorb carbon dioxide. The conversion module is used to perform a hydrogenation reaction between the desorbed carbon dioxide and the introduced hydrogen gas on the catalyst surface of the shell layer, generating liquid formic acid in situ and releasing heat of reaction. The regeneration module is used to assist the desorption of the surrounding core layer by utilizing the heat of reaction, forming a self-heating cycle that is initiated by photothermal reaction and maintained by chemical exothermic reaction until the adsorbent is completely regenerated. The generated liquid formic acid is discharged from the bottom of the tower and collected in a storage tank before switching back to adsorption mode, thus completing the self-heating regeneration, conversion and product collection cycle of a single tower.

9. An electronic device, characterized in that, Including processor and memory; The processor reads executable program code stored in the memory to run a program corresponding to the executable program code, so as to implement the method as described in any one of claims 1-7.

10. A non-transitory computer-readable storage medium having a computer program stored thereon, characterized in that, When the program is executed by the processor, it implements the method as described in any one of claims 1-7.

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