Moving bed temperature swing adsorption system and method

Abstract

The invention provides a moving bed temperature swing adsorption system and method which are applied to collaborative purification and carbon capture of aluminum anode roasting flue gas, and the system comprises a multi-temperature-zone moving bed reactor, a composite adsorbent circulation loop and a central control unit, the multi-temperature-zone moving bed reactor sequentially comprises a low-temperature adsorption zone, a medium-temperature catalytic adsorption zone and a high-temperature desorption regeneration zone from top to bottom; the high-temperature desorption regeneration area is provided with a heat exchange tube bundle, and high-temperature flue gas from an anode roasting furnace is introduced into the heat exchange tube bundle; the composite adsorbent circulating loop realizes circulating operation of composite adsorbent particles; the flue gas treatment flow path enables the aluminum anode roasting flue gas to be in countercurrent contact with the composite adsorbent particles; the CO2 product gas leading-out pipeline is used for leading out the generated CO2 product gas; the central control unit obtains the state parameters, obtains the optimal manipulated variable according to the state parameters, and carries out global optimization control based on the optimal manipulated variable, thereby reducing the energy consumption of the aluminum anode roasting flue gas treatment, and improving the utilization rate of the adsorbent.

Description

Technical Field

[0001] The present invention relates to the field of carbon capture control, and in particular to a moving bed temperature swing adsorption system and method. Background Art

[0002] As an important basic raw material industry in the world, the electrolytic aluminum industry accounts for an important proportion of its energy consumption and carbon emissions in the industrial field. In the electrolytic aluminum production process, pre-baked anodes for aluminum are indispensable key consumable materials, and the roasting process in its preparation process has become a major source of pollutant emissions and carbon emissions. The anode roasting process is usually carried out under high temperature conditions of about 1200°C. The raw anode material made of a mixture of petroleum coke and coal tar is heat-treated in a roasting furnace, and in this process, a flue gas with complex composition and high temperature is released. The flue gas contains a lot of CO2, and the volume fraction is usually between 5% and 15%, and is also mixed with SO2, NO x , HF, dust and typical organic pollutants such as polycyclic aromatic hydrocarbons produced by pyrolysis and volatilization of coal tar.

[0003] The current common technical approach for treating this type of high-temperature, complex flue gas is a multi-stage treatment process constructed with multiple independent units connected in series. A typical treatment process involves, in sequence, electrostatic precipitators (ESP) or bag filters to remove particulate matter, dry or wet desulfurization (FD) to remove sulfur dioxide, a selective catalytic reduction (SCR) system to remove nitrogen oxides, and finally, activated carbon and other adsorption devices to remove polycyclic aromatic hydrocarbons (PAHs) and dioxins. While these approaches are effective in controlling individual pollutants, they suffer from several significant shortcomings from a holistic system perspective. First, because each pollutant requires independent treatment equipment, the overall treatment system is complex, requires numerous devices, occupies a large area, and has high initial investment and capital costs. Second, there is a lack of thermal energy synergy and system integration between the various units. The flue gas undergoes multiple heating and cooling cycles between treatment units to adapt to their optimal operating temperatures, resulting in significant energy waste and low overall system efficiency. Furthermore, the existing multi-level governance processes often fail to incorporate carbon capture functions into the overall design. However, carbon capture, as a key link in addressing climate change, is particularly important in the current context of carbon peak and carbon neutrality.

[0004] When attempting to add a carbon capture step at the end of the above-mentioned traditional process, chemical absorption methods are often used, especially absorption processes based on amine solutions. Although amine washing technology is relatively mature in the field of post-combustion carbon capture, it faces serious challenges in treating roasting flue gas, as roasting flue gas contains SO2, NO x, HF and other acidic components, which will undergo irreversible side reactions with amine solution, causing rapid degradation of amine solution and the formation of corrosive by-products, which not only causes amine solution loss and increased operating costs, but also brings about problems such as equipment corrosion and secondary pollution. At the same time, the regeneration process of amine solution consumes a large amount of steam, and the unit CO2 capture energy consumption is usually as high as 3-4 GJ / ton, making the overall carbon capture process extremely expensive to operate. Some studies have attempted to use solid adsorbents such as molecular sieves, activated carbon and other materials to capture CO2. However, the recycling rate of adsorbent particles is low, which reduces the economic efficiency and availability.

[0005] In summary, the existing technology has not yet formed an integrated solution for achieving coordinated purification of flue gas treatment and efficient CO2 capture at the system level. It also lacks a technical path that can fully utilize the high-grade waste heat of the roasting furnace to reduce overall energy consumption, resulting in high energy consumption in aluminum anode roasting flue gas treatment and low adsorbent utilization.

[0006] In response to this problem, the present invention provides a moving bed temperature swing adsorption system and method to solve the above problem. Summary of the Invention

[0007] In order to solve the problems existing in the prior art, the present invention innovatively proposes a moving bed temperature swing adsorption system and method, which effectively solves the problems of high energy consumption and low adsorbent utilization rate in the treatment of aluminum anode roasting flue gas caused by the prior art, effectively reduces the energy consumption of aluminum anode roasting flue gas treatment and improves the adsorbent utilization rate.

[0008] The first aspect of the present invention provides a moving bed temperature-variable adsorption system, which is used for the coordinated purification and carbon capture of aluminum anode baking flue gas, including: a multi-temperature zone moving bed reactor, a composite adsorbent circulation loop, a flue gas treatment flow path, a CO2 product gas outlet pipeline, and a central control unit. The interior of the multi-temperature zone moving bed reactor includes a low-temperature adsorption zone, a medium-temperature catalytic adsorption zone and a high-temperature desorption and regeneration zone from top to bottom; the high-temperature desorption and regeneration zone is provided with a heat exchange tube bundle for directly introducing the high-temperature flue gas or hot air from the anode baking furnace into the heat exchange tube bundle to utilize industrial waste heat; the composite adsorbent circulation loop is used to add composite adsorbent particles from the top of the multi-temperature zone moving bed reactor, so that the composite adsorbent particles move from top to bottom under the action of gravity. , passing through the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption regeneration zone in turn, and discharging the regenerated high-temperature composite adsorbent particles from the bottom of the multi-temperature zone moving bed reactor, and circulating them back to the top of the multi-temperature zone moving bed reactor to realize continuous closed-loop operation; the flue gas treatment flow path is used to introduce the aluminum anode roasting flue gas from the lower part of the multi-temperature zone moving bed reactor, so that the aluminum anode roasting flue gas contacts with the composite adsorbent particles in countercurrent and flows from bottom to top; the CO2 product gas outlet pipeline is used to lead out the CO2 product gas generated in the high-temperature desorption regeneration zone; the central control unit is used to obtain the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and perform global optimization control according to the state parameters.

[0009] A second aspect of the present invention provides a moving bed temperature swing adsorption method, which is implemented based on the moving bed temperature swing adsorption system described in the first aspect of the present invention and is applied to the coordinated purification and carbon capture of aluminum anode baking flue gas, comprising: The composite adsorbent particles are continuously added from the top of the multi-temperature zone moving bed reactor, and the composite adsorbent particles move from top to bottom under the action of gravity, passing through the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone in sequence; The flue gas treatment flow path introduces the aluminum anode baking flue gas from the lower part of the multi-temperature zone moving bed reactor, so that the aluminum anode baking flue gas contacts with the composite adsorbent particles in countercurrent flow and flows from bottom to top; In the low-temperature adsorption zone, CO2 in the flue gas from the aluminum anode baking is adsorbed on the composite adsorbent particles; In the medium-temperature catalytic adsorption zone, organic pollutants in the flue gas from aluminum anode baking are catalytically oxidized under the action of the catalytic components of the composite adsorbent particles, while achieving stable adsorption of acidic gases in the flue gas from aluminum anode baking; The composite adsorbent particles carrying the adsorbed components enter the high-temperature decomposition and regeneration zone, and use the external heat source or the direct high-temperature waste heat of the roasting furnace to desorb the adsorbed CO2, and the CO2 product gas outlet pipeline will lead out the generated CO2 product gas; The high-temperature composite adsorbent particles after regeneration in the composite adsorbent circulation loop are discharged from the bottom of the multi-temperature zone moving bed reactor and circulated back to the top of the multi-temperature zone moving bed reactor to achieve continuous closed-loop operation; The central control unit obtains the state parameters of the multi-temperature zone moving bed reactor, composite adsorbent circulation loop, flue gas treatment flow path, and CO2 product gas outlet pipeline, and performs global optimization control based on the state parameters.

[0010] The technical solution adopted by the present invention includes the following technical effects: 1. The technical solution of the present invention integrates multiple functions such as flue gas treatment and purification and CO2 capture into a single moving bed reactor, replacing the traditional multi-tower series system, which can shorten the process flow, reduce the number of equipment and floor space, and lower the initial investment of the project; construct different temperature reaction areas in the reactor, and use the high-temperature waste heat of the anode roasting furnace itself as the main energy source for CO2 desorption in the high-temperature desorption regeneration area to achieve cascade utilization of energy. Compared with the amine washing method that requires a large amount of external steam, the regeneration energy consumption is extremely low, which reduces the CO2 capture cost; and through the composite adsorbent circulation loop, the continuous closed-loop operation of the adsorbent is realized, effectively solving the problems of high energy consumption and low adsorbent utilization rate in the flue gas treatment of aluminum anode roasting caused by the existing technology, effectively reducing the energy consumption of the flue gas treatment of aluminum anode roasting and improving the adsorbent utilization rate.

[0011] 2. In the technical solution of the present invention, the low-temperature adsorption zone is located at the upper part of the multi-temperature zone moving bed reactor, and is used for chemical adsorption of CO2 in the low-temperature range; the medium-temperature catalytic adsorption zone is located in the middle part of the multi-temperature zone moving bed reactor, and is used for catalytic oxidation of organic pollutants in the flue gas from the aluminum anode roasting in the medium-temperature range and adsorption of sulfur oxides in the flue gas from the aluminum anode roasting; the high-temperature desorption and regeneration zone is located at the lower part of the multi-temperature zone moving bed reactor, and is used for desorbing CO2 and regenerating the adsorbent in the high-temperature range, which not only efficiently captures CO2, but also efficiently removes organic pollutants and SO2 at the same time, realizing integrated deep purification of flue gas and meeting increasingly stringent environmental emission standards; and an isolation component is provided between the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and / or independent heat exchangers are respectively provided at positions corresponding to different temperature zones on the outer wall of the multi-temperature zone moving bed reactor to slow down the axial back mixing of the solid phase and the gas phase, help maintain the temperature gradient of the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and ensure the treatment efficiency of the flue gas from the aluminum anode roasting.

[0012] 3. In the technical solution of the present invention, an adsorbent distributor for ensuring uniform contact between the solid and gas phases is provided on the top of the multi-temperature zone moving bed reactor. The adsorbent distributor is a conical spreading plate, and the cone is arranged below the solid inlet. The particles fall on the cone and naturally spread around, which is used to evenly disperse the adsorbent over the entire cross-section of the multi-temperature zone moving bed reactor. It can ensure that the solid particles move from top to bottom in a stable manner, thereby ensuring the treatment efficiency of the aluminum anode roasting flue gas.

[0013] 4. The technical solution of the present invention is that the composite adsorbent particles include a composite adsorbent core and a composite adsorbent shell. The composite adsorbent core is an alkaline adsorption carrier with a high specific surface area, loaded with alkali metal or alkaline earth metal oxides or salts, and can efficiently and reversibly chemically adsorb CO2 at low temperatures; the composite adsorbent shell is composed of a layer of porous, acid-resistant, and heat-stable catalytic material, loaded with active components for catalytic oxidation of organic pollutants, which is not only used to catalytically degrade organic pollutants, but also can physically protect the CO2 adsorption active sites of the composite adsorbent core, solving the problems of easy clogging, easy poisoning, and short life of traditional adsorbents, and reducing replacement costs and operational complexity.

[0014] 5. The central control unit in the technical solution of the present invention includes a parameter measurement module, an MPC controller and an execution module. The parameter measurement module is used to measure the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and send the measured state parameters to the MPC controller. The MPC controller is used to obtain manipulated variables based on the state parameters and the controlled variables, and control the execution module based on the obtained manipulated variables, so that the operating performance of the entire moving bed temperature-variable adsorption system is globally optimized, can adapt to changes in working conditions, and can achieve long-term, stable and economical optimal operation, thereby improving the reliability and automation level of the system.

[0015] It should be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without any creative work.

[0017] Figure 1 This is a schematic diagram of the structure of the system in Example 1 of the present invention; Figure 2 Schematic diagram of the internal structure and temperature zone division of the multi-temperature zone moving bed reactor in the system of Example 1 of the present invention; Figure 3 Schematic diagram of the microstructure of the composite adsorbent particles with a core-shell structure in the system of Example 1 of the present invention; Figure 4 Schematic diagram of an intelligent control system based on an MPC controller in a system of Example 1 of the present invention; Figure 5 Schematic diagram of the working process of the MPC controller in the central control unit in the system of Example 1 of the solution of the present invention; Figure 6 This is a schematic flow chart of the method of Example 2 in the scheme of the present invention.

[0018] Figure 1 Legend: 1. Multi-temperature-zone moving bed reactor; 2. Flue gas inlet; 3. Purified flue gas outlet; 4. Solid flow control valve; 5. Adsorbent lifting device; 6. Heat exchange tube bundle; 7. CO2 product gas outlet pipeline; 8. Central control unit; 101. Calcination furnace; 102. Adsorbent lifting device motor; 103. Adsorbent cooler; 104. Adsorbent flow transmitter; 105. Cooling and water separator; 106. Flue gas outlet temperature transmitter; 107. Flue gas outlet concentration analyzer; 108. Flue gas inlet temperature transmitter; 109. Flue gas inlet flow transmitter; 110. Flue gas inlet concentration analyzer; 111. Condensate; 112. High-purity CO2 product; 113. Waste heat flue gas after cooling; Figure 2 Legend: 9, high-temperature waste heat interface; 10, composite adsorbent particles; 11, low-temperature adsorption zone; 12, medium-temperature catalysis-adsorption zone; 13, high-temperature desorption-regeneration zone; 14, solid collector; 201, adsorbent distributor; Figure 3 Legend: 141, composite adsorbent core; 142, composite adsorbent shell; 143, CO2 molecule; 144, H2O molecule; 145, PAH molecule; 146, SO2 molecule; Figure 4 Legend: 15. MPC controller; 16. Dynamic kinetic model; 17. Parameter measurement module; 18. Execution module; 19. Moving bed temperature swing adsorption system; 20. Optimizer. DETAILED DESCRIPTION

[0019] In order to clearly illustrate the technical features of this solution, the present invention is described in detail below through specific implementation methods and in conjunction with the accompanying drawings. The disclosure below provides many different embodiments or examples for realizing different structures of the present invention. In order to simplify the disclosure of the present invention, the components and settings of specific examples are described below. In addition, the present invention may repeat reference numbers and / or letters in different examples. This repetition is for the purpose of simplicity and clarity and does not itself indicate the relationship between the various embodiments and / or settings discussed. It should be noted that the components illustrated in the accompanying drawings are not necessarily drawn to scale. The present invention omits descriptions of well-known components and processing technologies and processes to avoid unnecessary limitations on the present invention.

[0020] Example 1 like Figure 1-Figure 2 As shown, the present invention provides a moving bed temperature swing adsorption system, which is applied to the coordinated purification and carbon capture of aluminum anode baking flue gas, comprising: a multi-temperature zone moving bed reactor 1, a composite adsorbent circulation loop, a flue gas treatment flow path, a CO2 product gas outlet pipeline 7, and a central control unit 8. The interior of the multi-temperature zone moving bed reactor comprises, from top to bottom, a low-temperature adsorption zone 11, a medium-temperature catalytic adsorption zone 12, and a high-temperature desorption and regeneration zone 13; the high-temperature desorption and regeneration zone 13 is provided with a heat exchange tube bundle 6 (high-temperature zone heat exchanger) for directly introducing high-temperature flue gas or hot air from the anode baking furnace 101 into the heat exchange tube bundle 6 to utilize industrial waste heat; the composite adsorbent circulation loop is used to add composite adsorbent particles 10 from the top of the multi-temperature zone moving bed reactor 1, so that the composite adsorbent particles 10 are moved from top to bottom under the action of gravity. It moves downward, passing through the low-temperature adsorption zone 11, the medium-temperature catalytic adsorption zone 12 and the high-temperature desorption regeneration zone 13 in turn, and the regenerated high-temperature composite adsorbent particles 10 are discharged from the bottom of the multi-temperature zone moving bed reactor 1 and circulated back to the top of the multi-temperature zone moving bed reactor 1 to achieve continuous closed-loop operation; the flue gas treatment flow path is used to introduce the aluminum anode roasting flue gas from the lower part of the multi-temperature zone moving bed reactor 1, so that the aluminum anode roasting flue gas is in countercurrent contact with the composite adsorbent particles 10 and flows from bottom to top; the CO2 product gas outlet pipeline 7 is used to lead out the CO2 product gas generated in the high-temperature desorption regeneration zone 13; the central control unit 8 is used to obtain the state parameters of the multi-temperature zone moving bed reactor 1, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline 7, and perform global optimization control according to the state parameters.

[0021] The multi-temperature-zone moving bed reactor 1 may be a vertical multi-temperature-zone moving bed reactor capable of naturally forming and stably maintaining a significant temperature gradient in the vertical direction. The reactor is divided from top to bottom into at least three functionally distinct zones, including a low-temperature adsorption zone 11, a medium-temperature catalytic adsorption zone 12, and a high-temperature desorption and regeneration zone 13. The low-temperature adsorption zone 11 is located at the top of the multi-temperature-zone moving bed reactor 1 and is used for chemically adsorbing CO2 at low temperatures (100-200°C). In the low-temperature adsorption zone 11, the pretreated and cooled aluminum anode baking flue gas contacts the most active low-temperature composite adsorbent particles 10 added from the top. The CO2 in the aluminum anode baking flue gas is efficiently chemically adsorbed by the alkaline active sites on the cores of the composite adsorbent particles 10. The intermediate-temperature catalytic adsorption zone 12 is located in the middle of the multi-temperature-zone moving bed reactor 1 and is used to catalytically oxidize organic pollutants (PAHs, polyaromatic hydrocarbons) in the flue gas from the aluminum anode roasting process and adsorb sulfur oxides in the flue gas from the aluminum anode roasting process within a medium temperature range (200-350°C). The medium temperature range (200-350°C) not only meets the activation energy required for the catalytic oxidation of PAHs, but also facilitates the stable chemical adsorption of acidic gases, protecting the CO2 adsorbent from poisoning. Specifically, in the intermediate-temperature catalytic adsorption zone, the higher-temperature flue gas from the aluminum anode roasting process contacts the downwardly moving composite adsorbent particles 10. Organic pollutants such as polycyclic aromatic hydrocarbons (PAHs) remaining in the flue gas and potentially carried on the adsorbent surface are deeply catalytically oxidized into harmless CO2 and H2O by the catalytic components of the composite adsorbent particles 10. Simultaneously, this temperature range facilitates the stable chemical adsorption of acidic gases such as sulfur dioxide (SO2) and hydrogen fluoride (HF) on the composite adsorbent particles 10, thereby protecting downstream CO2 adsorption sites. The high-temperature desorption and regeneration zone is located at the bottom of the multi-temperature zone moving bed reactor and is used to desorb CO2 and regenerate the adsorbent in a high-temperature range (400-650°C). The heat is provided by the built-in heat exchange tube bundle 6. The system is preferentially connected to the high-temperature flue of the anode baking furnace 101 through the high-temperature waste heat interface 9 to realize waste heat utilization.

[0022] The stable temperature of each temperature zone in the multi-temperature zone moving bed reactor 1 is achieved by combining one or more of the following methods: One method is to install internal components (isolation components) between the temperature zones, such as conical baffles or gas redistributors, to slow down the axial backmixing of the solid and gas phases and help maintain the temperature gradient.

[0023] One method is to provide independent jacketed heat exchangers at positions on the outer wall of the multi-temperature zone moving bed reactor 1 corresponding to different temperature zones to achieve precise temperature control.

[0024] One method is to directly implant a heat exchange tube bundle 6 (i.e., a shell and tube heat exchanger made of high-temperature resistant alloy, whose tube side directly introduces the original hot flue gas with a temperature higher than 700°C from the anode baking furnace) inside the multi-temperature zone moving bed reactor 1. In particular, the high-temperature flue gas or hot air from the anode baking furnace 101 is directly introduced into the heat exchange tube bundle 6 in the high-temperature desorption-regeneration zone, thereby utilizing high-grade industrial waste heat in a direct and efficient manner. Preferably, heat exchange tube bundles 6 can also be set in both the low-temperature adsorption zone 11 and the medium-temperature catalytic adsorption zone 12 to ensure the temperature of each temperature zone and slow down the backmixing of the solid and gas phases.

[0025] The present invention achieves cascaded energy utilization by integrating the heat exchange tube bundle 6 in the high-temperature desorption and regeneration zone 13 within the multi-temperature zone moving bed reactor 1. The large amount of thermal energy required by the high-temperature desorption and regeneration zone 13 is preferentially provided by the high-temperature waste heat interface 9 provided in this area, which is directly introduced into the high-temperature waste heat flue gas (usually with a temperature above 700°C) from the upstream roasting furnace 101 for heat exchange. This direct coupled utilization of energy returns the cooled waste heat flue gas 113 after heat exchange to the original flue, greatly reducing the system's external energy demand and operating costs. When it is monitored and predicted that the waste heat alone is insufficient to maintain the target temperature, the backup heat source is activated for supplementation. The entire temperature control process is executed by the central control unit 8 to achieve priority and maximum utilization of waste heat and minimized and precise supplementation of the backup heat source.

[0026] Another key point of the present invention is a specially designed core-shell composite adsorbent particle 10, the microscopic design concept of which is as follows: Figure 3 As shown, the adsorbent has clear functional divisions: its composite adsorbent core 141 is protected by the composite adsorbent shell 142, which enables functional specialization and performance optimization. The active component loaded thereon is preferably lithium silicate (Li4SiO4) with high selectivity and high capacity for CO2. This material is loaded on a high specific surface area carrier (such as γ-Al2O3), which can efficiently capture CO2 in low temperature areas and stably desorb in high temperature areas to achieve a long cycle; the outside of the composite adsorbent core 141 is coated with a porous, acid-resistant, and wear-resistant composite adsorbent shell 142. The composite adsorbent shell 142 has both active catalytic and physical and chemical barrier functions. The catalyst loaded thereon (preferably V2O5-WO3 / TiO2 or CeO2-MnO x ) can catalytically oxidize organic pollutants such as PAHs in flue gas into CO2 and H2O in the medium-temperature catalytic adsorption zone 12, thus avoiding poisoning of the adsorbent. At the same time, its dense, porous structure and acid-resistant materials (such as TiO2 and ZrO2) effectively intercept tar and dust, and adsorb acidic gases such as SO2 and HF, providing a clean operating microenvironment for the composite adsorbent core 141.

[0027] The top of the multi-temperature zone moving bed reactor 1 is provided with an adsorbent distributor 201 for uniformly contacting the solid and gas phases. The adsorbent distributor 201 can be a conical spreading plate, with the cone provided below the solid inlet. The particles falling on the cone naturally spread out in all directions, and is used to evenly disperse the adsorbent over the entire cross-section of the multi-temperature zone moving bed reactor to ensure that the solid particles move from top to bottom in a stable manner. Preferably, the structure of the adsorbent distributor 201 can be a conical spreading plate with a baffle, with a fixed cone provided below the solid inlet. The particles falling on the cone naturally spread out in all directions. The cone can be provided with guide ribs or baffles to further improve the uniformity of distribution. The function is to evenly spread the recycled solid adsorbent over the entire cross-section of the reactor to ensure that the solid particles move from top to bottom in a stable "plug flow" manner. A solid collector is provided at the bottom to collect the composite adsorbent particles 10.

[0028] The composite adsorbent particle 10 includes a composite adsorbent core 141 (adsorption core) and a composite adsorbent shell 142 (catalytic shell). The composite adsorbent core 141 is an alkaline adsorption carrier with a high specific surface area (preferably γ-Al2O3, SiO2 or mesoporous molecular sieve), loaded with alkali metal or alkaline earth metal oxides or salts (preferably lithium carbonate, potassium carbonate, calcium oxide or particularly preferably lithium silicate Li4SiO4), which serves as a CO2 adsorption active center for efficient and reversible chemical adsorption of CO2 at low temperatures; the composite adsorbent shell 142 is composed of a layer of porous, acid-resistant, and thermally stable catalytic material (preferably TiO2, ZrO2 or activated carbon), loaded with active components for catalytic oxidation of organic pollutants (preferably V2O5-WO3 / TiO2, CeO2-MnO x Composite oxides, or supported precious metal Pt, Pd nanoparticles), are used to play the dual role of catalytic degradation and physical protection of the composite adsorbent core 141, avoiding the clogging of the adsorbent pores by sticky substances such as polycyclic aromatic hydrocarbons (PAHs) and tar in the roasting flue gas, thereby causing the adsorbent to become inactivated or even non-regenerable, seriously shortening its service life and reducing its economic efficiency and operability.

[0029] The composite adsorbent circulation loop includes an adsorbent lifting device 5 (which may be a bucket elevator, a pneumatic conveying device or a screw conveyor) arranged at the top of the multi-temperature-zone moving bed reactor 1 and a solid flow control valve 4 arranged at the bottom of the multi-temperature-zone moving bed reactor 1. The solid flow control valve 4 is used to discharge the regenerated composite adsorbent particles 10 from the bottom of the multi-temperature-zone moving bed reactor 1 to realize the closed-loop circulation operation of the composite adsorbent particles 10. The adsorbent lifting device 5 is used to circulate the discharged composite adsorbent particles 10 from the bottom of the multi-temperature-zone moving bed reactor 1 back to the top of the multi-temperature-zone moving bed reactor 1.

[0030] Specifically, in steady-state operation, the roasting flue gas to be treated from the upstream roasting furnace 101 enters the multi-temperature zone moving bed reactor 1 through the flue gas inlet 2 at the bottom of the system after preliminary dust removal, and flows from bottom to top. At the same time, the core-shell structure composite adsorbent particles 10, whose microstructure is as follows Figure 3 As shown, the adsorbent is delivered to the top of the multi-temperature zone moving bed reactor 1 by the adsorbent lifting device 5 located at the top of the system. Under the action of gravity, these composite adsorbent particles 10 form a solid bed that slowly moves downward at a controllable rate, and conducts efficient countercurrent mass transfer and heat transfer with the rising flue gas. In the process of the flue gas passing upward through the moving bed, the various pollutants and carbon dioxide contained in it are collaboratively removed in layers and temperature zones. Finally, the clean flue gas after deep purification is discharged from the purified flue gas outlet 3 at the top of the reactor, and its outlet temperature and component concentration are monitored online by the flue gas outlet temperature transmitter 106 and the flue gas outlet concentration analyzer 107, respectively. In contrast, the composite adsorbent particles 10 complete the low-temperature adsorption of CO2, the medium-temperature catalytic degradation of polycyclic aromatic hydrocarbons (PAHs), and the adsorption of acidic gases such as SO2 (SO2 molecules 146) and HF in the process of moving downward. Among them, the medium-temperature catalytic adsorption zone 12 can catalytically degrade polycyclic aromatic hydrocarbons (PAHs, i.e., PAH molecules 145) into CO2 and water (H2O molecules 144) under the action of the composite adsorbent particles 10. When the adsorbent particles saturated with adsorption move to the high-temperature desorption regeneration zone 13 at the bottom of the multi-temperature zone moving bed reactor, their chemical adsorption is carried out under the action of high-grade thermal energy. The CO2 is desorbed, forming a high-concentration (high-purity) CO2 product gas (CO2 molecules 143). This CO2-rich gas is discharged through the laterally arranged CO2 product gas outlet pipeline 7 and flows through an external cooling and water separator 105 for cooling and dehydration. After removing the condensed water 111, a high-purity CO2 product 112 is obtained for subsequent storage or utilization. The regenerated high-temperature adsorbent particles are discharged from the bottom of the multi-temperature zone moving bed reactor 1 through a solid flow control valve 4 precisely controlled by the central control unit 8. The flow rate is monitored in real time by the adsorbent flow transmitter 104. The discharged hot adsorbent enters the adsorbent cooler 103 for cooling and is then lifted back to the top of the multi-temperature zone moving bed reactor 1 by the adsorbent lifting device 5, thus completing a continuous, uninterrupted closed-loop cycle. The stable and optimized operation of the entire system depends on a central control unit 8, which comprehensively integrates sensor signals from various parts of the system, including but not limited to the flue gas inlet temperature transmitter 108, the flue gas inlet flow transmitter 109 and the flue gas inlet concentration analyzer 110, and through advanced control algorithms, sends optimal control instructions to the actuators in the system (such as the solid flow control valve 4, the adsorbent lifting device motor 102, the high-temperature zone heat exchanger 6, etc.), realizing the automation and intelligent regulation of the entire process.

[0031] Among them, such as Figure 4 As shown, the central control unit 8 includes a parameter measurement module 17, an MPC controller 15 and an execution module 18. The parameter measurement module 17 is used to measure the state parameters of the multi-temperature zone moving bed reactor 1, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline 7, and send the measured state parameters to the MPC controller 15. The MPC controller 15 is used to obtain manipulated variables based on the state parameters and the controlled variables, and control the execution module based on the obtained manipulated variables, so that the operating performance of the entire moving bed temperature swing adsorption system is globally optimized; wherein, the execution module 18 includes a solid flow control valve 4 and a heat exchange tube bundle 6 in the high-temperature desorption regeneration zone.

[0032] The controlled variables (CVs) of the MPC controller 15 are: the concentrations of CO2 and organic pollutants (PAHs) in the purified flue gas at the purified flue gas outlet 3 of the multi-temperature-zone moving bed reactor, and the temperature of key points in each temperature zone within the multi-temperature-zone moving bed reactor (i.e., the temperature distribution of detection points uniformly distributed axially within each temperature zone); The manipulated variables (MVs) of the MPC controller 15 are: the set value of the solid flow control valve 4 for determining the adsorbent circulation rate, and the heat load set value supplied to the heat exchange tube bundle 6 in the high-temperature desorption regeneration zone; preferably, it can also include the set value of the flue gas flow control valve for determining the flue gas flow rate; the control input sequence (manipulated variables) control parameters include the adsorbent circulation rate and the heat load set value of the high-temperature desorption regeneration zone. The adsorbent circulation rate is precisely controlled by adjusting the rotation speed of the solid flow control valve 4 at the bottom of the reactor. It determines the solid-gas contact ratio of the system and affects the mass transfer and heat transfer efficiency; the heat load set value of the high-temperature desorption regeneration zone 13 is achieved by controlling the output power of the external backup heat source, providing the energy required for CO2 desorption and catalyst regeneration, ensuring that the desorption temperature is maintained in the target range, and ensuring the regeneration effect and continuous operation capability of the system.

[0033] The state parameters include the concentration of flue gas components at the inlet and outlet of the multi-temperature zone moving bed reactor, the temperature of key points in each temperature zone, the adsorbent circulation rate, and the flue gas inlet flow rate.

[0034] The parameter measurement module 17 is a general term for various measurement components in the system. Figure 1 These sensors include, but are not limited to: an adsorbent flow transmitter 104 for measuring adsorbent circulation rate; a flue gas outlet temperature transmitter 106 and a flue gas outlet concentration analyzer 107 for measuring the state of the purified flue gas; a flue gas inlet temperature transmitter 108, a flue gas inlet flow transmitter 109, and a flue gas inlet concentration analyzer 110 for measuring inlet flue gas disturbance; and multi-point thermocouples located within the moving bed reactor 1 for measuring the axial temperature distribution in each temperature zone. These sensors collectively provide real-time data on the system's operating status to the MPC controller 15.

[0035] Specifically, if Figure 5 As shown, the manipulated variables are obtained according to the state parameters and the controlled variables, and the execution modules are controlled according to the manipulated variables, so that the operating performance of the entire moving bed temperature swing adsorption system is globally optimized. Specifically, the following steps are performed: S11, using a parameter measurement module to collect the concentration of flue gas components at the inlet and outlet of the multi-temperature zone moving bed reactor, the temperature of key points in each temperature zone, the adsorbent circulation rate, and the flue gas inlet flow rate as input parameters for the MPC controller; The input parameters can be operating state parameters, which include inlet disturbance variables, internal process variables, and outlet feedback variables. Inlet disturbance variables mainly include inlet flue gas flow rate, inlet flue gas temperature, and inlet flue gas component concentration; internal process variables include: axial key point temperature of each temperature zone, adsorbent circulation rate, and adsorbent loading; outlet feedback variables include: outlet flue gas component concentration and outlet flue gas temperature.

[0036] S12, at each control moment, by inputting parameter information, manipulated variables, and a dynamic kinetic model (a system mechanism model of mass transfer-heat transfer-reaction coupled kinetics), predicting the dynamic behavior trajectory of the performance indicators of the moving bed temperature swing adsorption system over a future period of time; wherein the performance indicators are determined based on the controlled variables, including CO2 capture rate, pollutant removal rate, and external energy consumption; the CO2 capture rate is determined based on the concentration of CO2 in the purified flue gas at the purified flue gas outlet 3 of the multi-temperature zone moving bed reactor; the pollutant removal rate is determined based on the concentration of organic pollutants and SO2 in the purified flue gas at the purified flue gas outlet 3 of the multi-temperature zone moving bed reactor; and the external energy consumption is determined based on the temperature distribution of key points in each temperature zone within the multi-temperature zone moving bed reactor; Among them, the CO2 capture rate is calculated based on the concentration of CO2 in the purified flue gas at the purified flue gas outlet 3 of the multi-temperature zone moving bed reactor, the pollutant removal rate is calculated based on the concentration of organic pollutants and SO2 in the purified flue gas at the purified flue gas outlet 3 of the multi-temperature zone moving bed reactor, and the external energy consumption is calculated based on the temperature distribution of the axial key points of each temperature zone in the multi-temperature zone moving bed reactor. All of these are existing calculation methods and are not limited in the embodiments of the present invention.

[0037] Specifically, the dynamic kinetic model 16 includes a gas phase mass balance equation for describing the mass transfer of the gas phase in the multi-temperature zone moving bed reactor, a solid phase mass balance equation for describing the mass transfer of the solid phase in the multi-temperature zone moving bed reactor, a linear driving force model for describing the adsorption of CO2 in the multi-temperature zone moving bed reactor, a Langmuir-Hinshelwood model for describing the oxidation of organic pollutants (PAHs) in the medium-temperature catalytic adsorption zone in the multi-temperature zone moving bed reactor, a gas phase heat balance equation for describing the temperature management of the gas phase in the multi-temperature zone moving bed reactor, and a solid phase heat balance equation for describing the temperature management of the solid phase in the multi-temperature zone moving bed reactor; Among them, the gas phase mass balance equation is specifically: ; in, is the concentration of component i in the gas phase; is the gas phase flow rate; is the gas phase axial backmixing coefficient; is the external diffusion mass transfer coefficient; is the specific surface area; is the gas phase concentration on the surface of the composite adsorbent particles; z represents the axial coordinate of the multi-temperature zone moving bed reactor; g is the gas phase; Among them, the solid phase mass balance equation is specifically: ; in, is the adsorption amount of component i in the solid phase; is the back-mixing coefficient of the solid phase in the axial direction; is the solid phase migration rate; is the generation / consumption rate term of component i; s is the solid phase; The linear driving force model (i.e., double exponential linear driving force model, LDF Model) is specifically: ; in, is the adsorption rate of CO2 (mol / (s·m²)); is the total mass transfer coefficient in the linear driving force model (mol / (s·m²·Pa)); is the equilibrium adsorption capacity of CO2 (mol / g); is the current adsorption amount of CO2 (mol / g); The Langmuir-Hinshelwood model is specifically: ; in, is the catalytic oxidation rate of organic pollutants (mol / (s·m²)); is the catalytic reaction rate constant (mol / (s·m²·Pa)); is the adsorption constant of organic pollutants (1 / Pa); is the concentration of organic pollutants in the gas phase (mol / m³); is the adsorption constant of oxygen (1 / Pa); is the concentration of oxygen in the gas phase (mol / m³); The gas phase heat balance equation is specifically: ; in, is the gas phase void ratio; is the gas phase density (kg / m³); is the relative heat capacity of gas (J / (kg·K)); is the thermal conductivity of the gas phase (W / (m·K)); is the gas phase superficial velocity (m / s); is the solid-gas heat transfer coefficient (W / (m²·K)); is the specific surface area (m² / m³); is the gas phase temperature (K); is the solid phase temperature (K); The solid phase heat balance equation is specifically: ; in, is the solid phase density (kg / m³); is the solid specific heat capacity (J / (kg·K)); is the thermal conductivity of the solid phase (W / (m·K)); is the solid phase movement rate (m / s); is the solid-gas heat transfer coefficient (W / (m²·K)); is the reaction enthalpy change of the jth reaction process (chemical adsorption of CO2 (exothermic), desorption of CO2 (endothermic), catalytic oxidation of PAHs (strongly exothermic), chemical adsorption of SO2 and HF (exothermic)); is the reaction rate of the j-th reaction process (J / s); is the heat transfer term from the external heat source (power, unit W).

[0038] The prediction process is carried out within the MPC controller 15. It first obtains the current system state parameters from the parameter measurement module 17. Then, using the dynamic dynamics model 16 based on the mass and energy balance equations (an approximate model after the linearization of the linear state space model), it uses a fast numerical solution to forward deduction under the joint drive of an assumed future control action sequence (manipulated variables u) and a predicted external disturbance sequence d, thereby generating a set of dynamic trajectories of key performance indicators x2 (such as pollutant concentration, capture rate and energy consumption) covering the future time window.

[0039] That is, MPC substitutes the above input state parameters into its internal dynamic kinetic model 16, and performs a forward simulation starting from the current time t, to calculate the evolution trajectory of all state parameters of the system in the future prediction time domain (P); Specifically, the state is first predicted. At the next control time t+1, the state variables measured at the current time t, the implemented control inputs, and the currently measured disturbances are used to predict the state value at the current time through the dynamic dynamics model 16 (directly output as the state variable prediction value).

[0040] ; ; ; in, For the The performance indicator prediction value at time For the The predicted value of the controlled variable at time , For the The predicted value of the state variable at time , For the current The measured value of the state variable at the moment; For the current The actual value of the manipulated variable at the moment; For the The measured value of the disturbance variable at the moment; F, B, C1, and C2 are the system state matrix, input matrix, first output matrix, and second output matrix respectively; E is the influence matrix of the disturbance variable on the state variable.

[0041] It should be noted that in this plan 、 Represents the functional relationship between the performance index and the controlled variable at the next moment, 、 Indicates the functional relationship between the controlled variable and the state variable at the next moment, 、 、 、 It represents the functional relationship between the state variable at the next moment and the state variable, manipulated variable, and disturbance variable at the current moment, that is, the predicted value of the performance indicator at the next moment is obtained by the predicted value of the controlled variable at the next moment, the predicted value of the controlled variable at the next moment is obtained by the predicted value of the state variable at the next moment, and the predicted value of the state variable at the next moment is obtained by the measured value of the state variable, manipulated variable value, and disturbance variable at the current moment.

[0042] disturbance variable Obtained through online system measurements, it serves as a known feedforward input to the dynamic kinetic model 16 at the current control moment t, participating in the prediction and optimization of future control effects. The disturbance impact matrix E directly links the impact of external disturbances with changes in the system's internal state. This matrix is ​​also derived from the original state balance equation through linearization during the modeling process. For example, changes in the inlet flue gas flow rate (a component of the disturbance variable d) will directly affect the gas phase flow rate term in the mass conservation equation, and this impact is reflected in the specific element values ​​of matrix E. During the prediction process, the MPC controller 15 substitutes the real-time measurement d(t) into the dynamic kinetic model 16 and calculates the direct impact of the disturbance on the state at the next moment through the term Ed(t), allowing the MPC controller 15 to react in advance and achieve feedforward suppression of the disturbance.

[0043] S13: Construct an optimization objective function based on CO2 capture rate, pollutant removal rate, and external energy consumption. Under the condition that all preset constraints are met, solve the optimization problem online and calculate the optimal manipulated variables. Among them, the optimization objective function is specifically: ; Among them, J is the optimization objective function value, is the carbon capture weight, is the pollutant purification weight, is the external operation energy consumption weight; is the capture rate; The concentration of organic pollutants at the outlet of the purified flue gas of the multi-temperature zone moving bed reactor; is the external energy cost; Weight factors in the objective function 、 、 It can be adjusted in real time according to the status of the system. The adjustment formulas are as follows: ; in, It is the pollutant purification weight calculated in real time; The basic weight for pollutant purification represents the basic emphasis on pollutant control under normal operation; is the pollutant concentration measured in real time by the outlet concentration analyzer 107 or predicted by the dynamic kinetic model 16 within the prediction time domain; is the upper limit of pollutant emission concentration, which is a constant used as a constraint condition; and k are adjustable parameters, serving as gain and exponential coefficients, respectively, for fine-tuning the starting point and intensity of weight growth; ; in, External operation energy consumption weight calculated in real time; It is the external operating energy consumption basic weight, representing the general emphasis on energy conservation; Real-time working status of backup heat source; Real-time electricity price (yuan / kWh). In areas where time-of-use electricity prices are implemented, this value changes over time. is the conversion coefficient used to convert the electricity price to a level that matches other weights.

[0044] ; in, The carbon capture weight is calculated in real time; is the base weight for carbon capture, which is usually the highest of the three weights; Weight for pollutant purification A very large cap that can be reached, used for normalization.

[0045] The preset constraints specifically include: the adsorbent circulation rate is within the preset rate range, the adsorbent circulation rate change rate does not exceed the preset change rate threshold, the standby heat source power is within the preset power range, the temperature of each temperature zone is within the preset temperature range, the pressure drop of the multi-temperature zone moving bed reactor does not exceed the preset pressure drop threshold, the CO2 capture rate is not less than the preset capture rate threshold, and the pollutant emission concentration does not exceed the preset concentration threshold.

[0046] Specifically, the preset constraints are mainly divided into manipulated variable constraints, state variable constraints, and output variable constraints, as follows: Upper and lower limits of adsorbent circulation rate: ; in, To control the adsorbent circulation rate corresponding to time t, Preset the minimum value of the rate range for the adsorbent circulation rate, Preset the maximum value of the rate range for the adsorbent circulation rate; Adsorbent circulation rate change rate: ; in, is the adsorbent circulation rate change rate, is a preset change rate threshold value for the adsorbent circulation rate change rate; Upper and lower limits of standby heat source power: ; in, To control the standby heat source power corresponding to time t, is the minimum value of the preset power range of the standby heat source power, The maximum value of the preset power range for the backup heat source power; Temperature variation range of each temperature zone: ; in, is the first Temperature changes in each temperature zone, For the The minimum temperature change in each temperature zone, For the The maximum temperature change in each temperature zone; Reactor pressure drop constraint: ; in, To control the pressure drop of the multi-temperature zone moving bed reactor at time t, is the preset pressure drop threshold of the multi-temperature zone moving bed reactor corresponding to the control time t; Minimum CO2 capture rate: ; in, To control the CO2 capture rate corresponding to time t, It is the preset CO2 capture rate threshold; Maximum pollutant emission concentration: ; in, To control the pollutant emission concentration corresponding to time t, is a preset concentration threshold for pollutant emission concentrations; The optimizer 20 solves the problem as follows: At the beginning of each control cycle, the optimizer 20 first obtains the most accurate current system operating state (such as zone temperature and adsorbent loading) from the parameter measurement module 17 as the initial conditions for the optimization calculation. Subsequently, the optimizer initiates an iterative solution process. Using the system physical model 16 constructed based on mass and energy balance equations, it rapidly simulates a series of candidate future control input sequences (i.e., adsorbent circulation rate for the next P time steps, high-temperature zone temperature setpoints, etc.). This predicts the dynamic evolution of system performance indicators (carbon capture rate, pollutant concentration, energy consumption cost) over the entire future prediction horizon under different control strategies, as follows: The carbon capture rate is predicted by solving the coupled gas-solid mass balance equation and combining it with the linear driving force (LDF) model describing CO2 adsorption kinetics to calculate the CO2 concentration at the reactor outlet, thereby obtaining the capture rate. Among the control parameters, increasing the adsorbent circulation rate or increasing the heat load in the high-temperature zone to obtain a more thoroughly regenerated adsorbent can increase the adsorption driving force in the low-temperature adsorption zone and improve the capture rate. The carbon capture rate is predicted by solving the coupled gas-solid mass balance equation and combining it with the linear driving force (LDF) model describing CO2 adsorption kinetics to calculate the CO2 concentration at the reactor outlet, thereby obtaining the capture rate.

[0047] The MPC controller 15 uses a linear driving force (LDF) model to describe the CO2 transfer rate from the gas phase to the solid-phase adsorbent. This rate is proportional to the adsorption driving force, which is the difference between the equilibrium adsorption capacity at the current temperature and pressure and the actual adsorbent loading. Increasing the adsorbent circulation rate (a control parameter or manipulated variable) introduces more regenerated adsorbent with a low loading (operating state), thereby increasing the adsorption driving force. Increasing the heat load in the high-temperature zone (a control parameter or manipulated variable) enables more thorough adsorbent regeneration, reduces its initial loading, and indirectly increases the adsorption driving force. Both of these control parameters ultimately reduce the outlet CO2 concentration by increasing the adsorption rate, thereby improving the capture efficiency.

[0048] Pollutant concentrations are predicted by solving a mass balance equation, where the pollutant consumption rate is described by the Langmuir-Hinshelwood (LH) catalytic kinetic model. Among the control parameters, increasing the heat load in the high-temperature zone is crucial for raising the catalytic reaction temperature in the intermediate-temperature zone, exponentially accelerating the PAH oxidation rate and thereby reducing outlet pollutant concentrations. The outlet pollutant concentration primarily depends on the catalytic oxidation removal efficiency in the intermediate-temperature catalytic adsorption zone 12. A model predictive controller (MPC) predicts this process by solving the equation of state of a catalytic reaction kinetic model such as the Langmuir-Hinshelwood (LH) model. In this model, the catalytic reaction rate constant (k) is extremely sensitive to temperature, following the Arrhenius relationship, with the reaction rate increasing exponentially with increasing temperature. The heat load in the high-temperature desorption and regeneration zone 13 determines the operating temperature of the intermediate-temperature zone through heat conduction and convection. Increasing the heat load significantly increases the catalytic reaction rate, thereby reducing outlet pollutant concentrations. The adsorbent circulation rate plays a secondary regulatory role by influencing the catalyst residence time and system thermal balance.

[0049] Energy costs are predicted by solving the system's heat balance equation to calculate the standby heat source power (Qext) required to maintain the set temperature in the high-temperature zone. This power requirement is directly related to the heat required for CO2 desorption (proportional to the adsorbent circulation rate and its CO2 loading). The total primary energy cost is the sum of the standby heat source power consumption and the power consumption of the adsorbent booster 5 (proportional to the adsorbent circulation rate). Energy consumption is directly linked to control parameters through physical relationships: the energy consumption of the adsorbent booster 5 is approximately proportional to the adsorbent circulation rate; the standby heat source energy consumption is determined by solving the system's heat balance equation and is equal to the sum of the heat required for CO2 desorption (proportional to the adsorbent circulation rate and its CO2 loading) and system heat losses, minus the available calciner waste heat.

[0050] The optimizer 20 substitutes the dynamic behavior trajectories of the performance indicators of the moving bed temperature swing adsorption system in the future into the weighted multi-objective function J for quantitative evaluation, and systematically searches through the numerical optimization algorithm until the only one that can minimize the value of the objective function J is found.

[0051] S14, sends the optimal manipulated variables to the execution module, performs real-time, closed-loop optimization control on the moving bed temperature swing adsorption system, actively suppresses disturbances, and ensures that the system always operates in the best state.

[0052] Finally, the optimizer 20 sends the first control action in this optimal control sequence (manipulated variables) to the execution module 18 for implementation, discarding the rest of the sequence. When the next control cycle arrives, the entire "measurement-prediction-optimization" rolling process is repeated again based on the new system state.

[0053] The following describes a specific industrial application example to further illustrate the embodiments of the present invention. This example is applied to a roasting plant with an annual production capacity of 200,000 tons of aluminum prebaked anodes. The pretreated flue gas from the roasting furnace has a flow rate of 120,000 Nm³ / h, an inlet temperature of 160°C, and contains 12% CO₂, 800 ppm SO₂, 50 ppm HF, and 100 mg / Nm³ of PAHs. The performance targets set were a CO₂ capture rate of no less than 90%, and SO₂ and PAHs removal rates of no less than 90% and 95%, respectively.

[0054] In this embodiment, the key equipment selection and detailed parameters of the system are as follows: the material of the vertical multi-temperature zone moving bed reactor 1 is made of carbon steel shell and refractory material lining in consideration of corrosion and operating temperature, and the high-temperature zone components are made of heat-resistant stainless steel or higher-grade heat-resistant alloy. According to the calculation of the gas processing volume, the reactor diameter is determined to be 6 meters, and the total effective height is 25 meters. The internal temperature zones are specifically divided into: a low-temperature adsorption zone 11 with a height of 8 meters, the operating temperature of which is controlled at 140-180°C; a medium-temperature catalytic adsorption zone 12 with a height of 7 meters, the temperature of which is naturally balanced between 250-320°C; and a high-temperature desorption-regeneration zone 13 with a height of 6 meters, the operating temperature of which is strictly controlled at 600-650°C. Its heat energy is mainly provided by the high-temperature zone heat exchanger (heat exchange tube bundle 6) that directly introduces 750°C waste heat from the roasting furnace. The composite adsorbent 10 used has a physical form of 2-3 mm in diameter. The composite adsorbent core 141 is made of 20% Li4SiO4 active components prepared by the sol-gel method, and the composite adsorbent shell 142 is made of V2O5-WO3 / TiO2 catalytic components prepared by chemical vapor deposition and impregnation. The adsorbent circulation rate is precisely adjusted within the range of 20-30 tons / hour by a star-feeder-type solid flow control valve 4.

[0055] After the system enters stable operation, the MPC controller 15 in the central control unit 8 optimizes and regulates the system. To simulate its intelligent control effect, we set up a typical scenario: responding to a calciner fire change operation, which causes the inlet flue gas flow rate to drop by 20% over 10 minutes. First, the disturbance is immediately detected and reported by the flue gas inlet flow transmitter 109. Next, the model within the MPC controller 15 (a dynamic kinetic model) predicts that without intervention, the system will face the risk of over-purification and a temperature drop in the high-temperature zone. Based on this prediction, the optimizer immediately activates and makes a decision, developing a coordinated control plan. It gradually reduces the adsorbent circulation rate to match the reduced CO2 flux, while moderately increasing the standby electric heating power in the high-temperature zone to maintain a stable desorption temperature. Finally, the MPC controller 15 sends instructions to the actuator, precisely adjusting the setpoint of the solid flow control valve 4, which determines the adsorbent circulation rate, and the setpoint of the heat load supplied to the heat exchanger bundle in the high-temperature desorption regeneration zone. This ensures that all outlet indicators remain stable within the target range throughout the disturbance, demonstrating strong robustness and adaptability.

[0056] The technical solution of the present invention integrates multiple functions such as flue gas treatment and purification and CO2 capture into a single moving bed reactor, replacing the traditional multi-tower series system, which can shorten the process flow, reduce the number of equipment and floor space, and lower the initial investment of the project; construct different temperature reaction areas in the reactor, and use the high-temperature waste heat of the anode roasting furnace itself as the main energy source for CO2 desorption in the high-temperature desorption regeneration area to achieve cascade utilization of energy. Compared with the amine washing method that requires a large amount of external steam, the regeneration energy consumption is extremely low, which reduces the CO2 capture cost; and realizes continuous closed-loop operation of the adsorbent through a composite adsorbent circulation loop, effectively solving the problems of high energy consumption and low adsorbent utilization rate in aluminum anode roasting flue gas treatment caused by existing technologies, effectively reducing the energy consumption of aluminum anode roasting flue gas treatment and improving the adsorbent utilization rate.

[0057] In the technical solution of the present invention, the low-temperature adsorption zone is located at the upper part of the multi-temperature zone moving bed reactor, and is used for chemical adsorption of CO2 in the low-temperature range; the medium-temperature catalytic adsorption zone is located in the middle part of the multi-temperature zone moving bed reactor, and is used for catalytic oxidation of organic pollutants in the flue gas from the aluminum anode roasting in the medium-temperature range and adsorption of sulfur oxides in the flue gas from the aluminum anode roasting; the high-temperature desorption and regeneration zone is located at the lower part of the multi-temperature zone moving bed reactor, and is used for desorbing CO2 and regenerating the adsorbent in the high-temperature range, which not only efficiently captures CO2, but also efficiently removes organic pollutants and SO2 at the same time, realizing integrated deep purification of flue gas and meeting increasingly stringent environmental emission standards; and an isolation component is provided between the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and / or independent heat exchangers are respectively provided at positions corresponding to different temperature zones on the outer wall of the multi-temperature zone moving bed reactor to slow down the axial back mixing of the solid phase and the gas phase, help maintain the temperature gradient of the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and ensure the treatment efficiency of the flue gas from the aluminum anode roasting.

[0058] In the technical solution of the present invention, an adsorbent distributor for ensuring uniform contact between the solid and gas phases is provided on the top of the multi-temperature zone moving bed reactor. The adsorbent distributor is a conical spreading plate, and the cone is arranged below the solid inlet. The particles fall on the cone and naturally spread around, which is used to evenly disperse the adsorbent over the entire cross-section of the multi-temperature zone moving bed reactor. It can ensure that the solid particles move from top to bottom in a stable manner, thereby ensuring the treatment efficiency of the aluminum anode baking flue gas.

[0059] The composite adsorbent particles of the technical solution of the present invention include a composite adsorbent core and a composite adsorbent shell. The composite adsorbent core is an alkaline adsorption carrier with a high specific surface area, loaded with alkali metal or alkaline earth metal oxides or salts, and can efficiently and reversibly chemically adsorb CO2 at low temperatures; the composite adsorbent shell is a layer of porous, acid-resistant, and heat-stable catalytic material, loaded with active components for catalytic oxidation of organic pollutants, which is not only used to catalytically degrade organic pollutants, but also can physically protect the CO2 adsorption active sites of the composite adsorbent core, solving the problems of easy clogging, easy poisoning, and short life of traditional adsorbents, and reducing replacement costs and operational complexity.

[0060] The central control unit in the technical solution of the present invention includes a parameter measurement module, an MPC controller and an execution module. The parameter measurement module is used to measure the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and send the measured state parameters to the MPC controller. The MPC controller is used to obtain manipulated variables based on the state parameters and the controlled variables, and control the execution module based on the obtained manipulated variables, so that the operating performance of the entire moving bed temperature-variable adsorption system is globally optimized, can adapt to changes in operating conditions, and can achieve long-term, stable, and economical optimal operation, thereby improving the reliability and automation level of the system.

[0061] Example 2 like Figure 6 As shown, the technical solution of the present invention also provides a moving bed temperature swing adsorption method, which is implemented based on a moving bed temperature swing adsorption system in Example 1 and is applied to the coordinated purification and carbon capture of aluminum anode baking flue gas, including: S1, composite adsorbent particles are continuously added from the top of the multi-temperature zone moving bed reactor, so that the composite adsorbent particles move from top to bottom under the action of gravity, passing through the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption regeneration zone in sequence; S2, the flue gas treatment flow path introduces the aluminum anode baking flue gas from the lower part of the multi-temperature zone moving bed reactor, so that the aluminum anode baking flue gas contacts with the composite adsorbent particles in countercurrent flow and flows from bottom to top; S3, in the low-temperature adsorption zone, CO2 in the flue gas from the aluminum anode baking is adsorbed on the composite adsorbent particles; S4, in the medium-temperature catalytic adsorption zone, the organic pollutants in the flue gas from the aluminum anode baking are catalytically oxidized under the action of the catalytic components of the composite adsorbent particles, while achieving stable adsorption of acidic gases in the flue gas from the aluminum anode baking; S5, the composite adsorbent particles carrying the adsorbed components enter the high-temperature decomposition and regeneration zone, where the adsorbed CO2 is desorbed using an external heat source or the direct high-temperature waste heat of the calciner, and the CO2 product gas outlet pipeline leads the generated CO2 product gas out; S6, the high-temperature composite adsorbent particles after regeneration in the composite adsorbent circulation loop are discharged from the bottom of the multi-temperature zone moving bed reactor and circulated back to the top of the multi-temperature zone moving bed reactor to achieve continuous closed-loop operation; S7, the central control unit obtains the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and performs global optimization control based on the state parameters.

[0062] The specific implementation process of the central control unit is consistent with the working process in Example 1, and will not be described in detail in this embodiment.

[0063] The technical solution of the present invention integrates multiple functions such as flue gas treatment and purification and CO2 capture into a single moving bed reactor, replacing the traditional multi-tower series system, which can shorten the process flow, reduce the number of equipment and floor space, and lower the initial investment of the project; construct different temperature reaction areas in the reactor, and use the high-temperature waste heat of the anode roasting furnace itself as the main energy source for CO2 desorption in the high-temperature desorption regeneration area to achieve cascade utilization of energy. Compared with the amine washing method that requires a large amount of external steam, the regeneration energy consumption is extremely low, which reduces the CO2 capture cost; and realizes continuous closed-loop operation of the adsorbent through a composite adsorbent circulation loop, effectively solving the problems of high energy consumption and low adsorbent utilization rate in aluminum anode roasting flue gas treatment caused by existing technologies, effectively reducing the energy consumption of aluminum anode roasting flue gas treatment and improving the adsorbent utilization rate.

[0064] In the technical solution of the present invention, the low-temperature adsorption zone is located at the upper part of the multi-temperature zone moving bed reactor, and is used for chemical adsorption of CO2 in the low-temperature range; the medium-temperature catalytic adsorption zone is located in the middle part of the multi-temperature zone moving bed reactor, and is used for catalytic oxidation of organic pollutants in the flue gas from the aluminum anode roasting in the medium-temperature range and adsorption of sulfur oxides in the flue gas from the aluminum anode roasting; the high-temperature desorption and regeneration zone is located at the lower part of the multi-temperature zone moving bed reactor, and is used for desorbing CO2 and regenerating the adsorbent in the high-temperature range, which not only efficiently captures CO2, but also efficiently removes organic pollutants and SO2 at the same time, realizing integrated deep purification of flue gas and meeting increasingly stringent environmental emission standards; and an isolation component is provided between the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and / or independent heat exchangers are respectively provided at positions corresponding to different temperature zones on the outer wall of the multi-temperature zone moving bed reactor to slow down the axial back mixing of the solid phase and the gas phase, help maintain the temperature gradient of the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone, and ensure the treatment efficiency of the flue gas from the aluminum anode roasting.

[0065] In the technical solution of the present invention, an adsorbent distributor for ensuring uniform contact between the solid and gas phases is provided on the top of the multi-temperature zone moving bed reactor. The adsorbent distributor is a conical spreading plate, and the cone is arranged below the solid inlet. The particles fall on the cone and naturally spread around, which is used to evenly disperse the adsorbent over the entire cross-section of the multi-temperature zone moving bed reactor. It can ensure that the solid particles move from top to bottom in a stable manner, thereby ensuring the treatment efficiency of the aluminum anode baking flue gas.

[0066] The composite adsorbent particles of the technical solution of the present invention include a composite adsorbent core and a composite adsorbent shell. The composite adsorbent core is an alkaline adsorption carrier with a high specific surface area, loaded with alkali metal or alkaline earth metal oxides or salts, and can efficiently and reversibly chemically adsorb CO2 at low temperatures; the composite adsorbent shell is a layer of porous, acid-resistant, and heat-stable catalytic material, loaded with active components for catalytic oxidation of organic pollutants, which is not only used to catalytically degrade organic pollutants, but also can physically protect the CO2 adsorption active sites of the composite adsorbent core, solving the problems of easy clogging, easy poisoning, and short life of traditional adsorbents, and reducing replacement costs and operational complexity.

[0067] The central control unit in the technical solution of the present invention includes a parameter measurement module, an MPC controller and an execution module. The parameter measurement module is used to measure the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and send the measured state parameters to the MPC controller. The MPC controller is used to obtain manipulated variables based on the state parameters and the controlled variables, and control the execution module based on the obtained manipulated variables, so that the operating performance of the entire moving bed temperature-variable adsorption system is globally optimized, can adapt to changes in operating conditions, and can achieve long-term, stable, and economical optimal operation, thereby improving the reliability and automation level of the system.

[0068] Although the above describes the specific embodiments of the present invention in conjunction with the accompanying drawings, it is not intended to limit the scope of protection of the present invention. Those skilled in the art should understand that various modifications or variations that can be made by those skilled in the art on the basis of the technical solution of the present invention without any creative work are still within the scope of protection of the present invention.

Claims

1. A moving bed temperature swing adsorption system, characterized in that: It is used for the coordinated purification and carbon capture of aluminum anode baking flue gas, including: a multi-temperature zone moving bed reactor, a composite adsorbent circulation loop, a flue gas treatment flow path, a CO2 product gas outlet pipeline, and a central control unit. The interior of the multi-temperature zone moving bed reactor includes a low-temperature adsorption zone, a medium-temperature catalytic adsorption zone and a high-temperature desorption and regeneration zone from top to bottom; the high-temperature desorption and regeneration zone is provided with a heat exchange tube bundle for directly introducing the high-temperature flue gas or hot air from the anode baking furnace into the heat exchange tube bundle to utilize industrial waste heat; the composite adsorbent circulation loop is used to add composite adsorbent particles from the top of the multi-temperature zone moving bed reactor, so that the composite adsorbent particles move from top to bottom under the action of gravity, and pass through the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone in turn. The multi-temperature moving bed reactor has a medium-temperature catalytic adsorption zone and a high-temperature desorption regeneration zone, and the regenerated high-temperature composite adsorbent particles are discharged from the bottom of the multi-temperature zone moving bed reactor and circulated back to the top of the multi-temperature zone moving bed reactor to realize continuous closed-loop operation; the flue gas treatment flow path is used to introduce the aluminum anode roasting flue gas from the bottom of the multi-temperature zone moving bed reactor, so that the aluminum anode roasting flue gas contacts with the composite adsorbent particles in countercurrent and flows from bottom to top; the CO2 product gas outlet pipeline is used to lead out the CO2 product gas generated in the high-temperature desorption regeneration zone; the central control unit is used to obtain the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and perform global optimization control according to the state parameters.

2. The moving bed temperature swing adsorption system according to claim 1, characterized in that: The low-temperature adsorption zone is located at the upper part of the multi-temperature zone moving bed reactor and is used for chemical adsorption of CO2 in a low-temperature range; the medium-temperature catalytic adsorption zone is located in the middle part of the multi-temperature zone moving bed reactor and is used for catalytically producing organic pollutants in the flue gas from the alumina anode roasting process and adsorbing sulfur oxides in the flue gas from the aluminum anode roasting process in a medium-temperature range; the high-temperature desorption and regeneration zone is located at the lower part of the multi-temperature zone moving bed reactor and is used for desorbing CO2 and regenerating the adsorbent in a high-temperature range; An isolation component is provided between the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone to slow down the axial back-mixing of the solid phase and the gas phase and help maintain the temperature gradient of the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone; And / or, independent heat exchangers are respectively provided at positions on the outer wall of the multi-temperature zone moving bed reactor corresponding to different temperature zones to perform temperature control.

3. The moving bed temperature swing adsorption system according to claim 1, characterized in that: An adsorbent distributor for ensuring uniform contact between the solid and gas phases is provided on the top of the multi-temperature zone moving bed reactor. The adsorbent distributor is a conical spreading plate with the cone arranged below the solid inlet. The particles fall on the cone and naturally spread out to the surroundings, thereby evenly distributing the adsorbent over the entire cross-section of the multi-temperature zone moving bed reactor to ensure that the solid particles move from top to bottom in a stable manner.

4. The moving bed temperature swing adsorption system according to claim 1, characterized in that: The composite adsorbent particles include a composite adsorbent core and a composite adsorbent shell. The composite adsorbent core is an alkaline adsorption carrier with a high specific surface area, loaded with alkali metal or alkaline earth metal oxides or salts, and is used for efficient and reversible chemical adsorption of CO2 at low temperatures; the composite adsorbent shell is composed of a layer of porous, acid-resistant, and thermally stable catalytic material, loaded with active components for catalytic oxidation of organic pollutants, and is used to play the dual role of catalytic degradation and physical protection of the composite adsorbent core.

5. The moving bed temperature swing adsorption system according to claim 1, characterized in that: The composite adsorbent circulation loop includes an adsorbent lifting device arranged at the top of the multi-temperature zone moving bed reactor and a solid flow control valve arranged at the bottom of the multi-temperature zone moving bed reactor. The solid flow control valve is used to discharge the regenerated composite adsorbent particles from the bottom of the multi-temperature zone moving bed reactor to realize the closed-loop circulation operation of the adsorbent particles. The adsorbent lifting device is used to circulate the discharged composite adsorbent particles from the bottom of the multi-temperature zone moving bed reactor back to the top of the multi-temperature zone moving bed reactor.

6. The moving bed temperature swing adsorption system according to claim 5, characterized in that: The central control unit includes a parameter measurement module, an MPC controller, and an execution module. The parameter measurement module is used to measure the state parameters of the multi-temperature zone moving bed reactor, the composite adsorbent circulation loop, the flue gas treatment flow path, and the CO2 product gas outlet pipeline, and send the measured state parameters to the MPC controller. The MPC controller is used to obtain manipulated variables based on the state parameters and controlled variables, and control the execution module based on the obtained manipulated variables to achieve global optimization of the operating performance of the entire moving bed temperature swing adsorption system. The execution module includes a solid flow control valve and a heat exchange tube bundle in the high-temperature desorption and regeneration zone. The controlled variables of the MPC controller are: the concentrations of CO2 and organic pollutants in the purified flue gas at the purified flue gas outlet of the multi-temperature zone moving bed reactor, and the temperatures at key points in each temperature zone within the multi-temperature zone moving bed reactor. The manipulated variables of the MPC controller are: the set value for adjusting the solid flow control valve to determine the adsorbent circulation rate, and the set value for the heat load supplied to the heat exchange tube bundle in the high-temperature desorption and regeneration zone. The state parameters include the concentrations of flue gas components in the inlet and outlet of the multi-temperature zone moving bed reactor, the temperatures at key points in each temperature zone, the adsorbent circulation rate, and the flue gas inlet flow rate.

7. The moving bed temperature swing adsorption system according to claim 6, characterized in that: The manipulated variables are obtained according to the state parameters and the controlled variables, and the execution modules are controlled according to the manipulated variables, so that the operating performance of the entire moving bed temperature swing adsorption system is globally optimized. Specifically, the following are included: The parameter measurement module collects the concentration of flue gas components in the inlet and outlet of the multi-temperature zone moving bed reactor, the temperature of key points in each temperature zone, the adsorbent circulation rate, and the flue gas inlet flow rate as input parameters of the MPC controller; At each control moment, the dynamic behavior trajectory of the performance indicators of the moving bed temperature swing adsorption system over a future period of time is predicted by inputting parameter information, manipulated variables, and a dynamic kinetic model. The performance indicators are determined based on the controlled variables, including the CO2 capture rate, the pollutant removal rate, and the external energy consumption. The CO2 capture rate is determined based on the CO2 concentration in the purified flue gas at the purified flue gas outlet of the multi-temperature zone moving bed reactor. The pollutant removal rate is determined based on the concentrations of organic pollutants and SO2 in the purified flue gas at the purified flue gas outlet of the multi-temperature zone moving bed reactor. The external energy consumption is determined based on the temperature distribution of key points in each temperature zone within the multi-temperature zone moving bed reactor. Construct an optimization objective function based on CO2 capture rate, pollutant removal rate, and external energy consumption. Under the condition that all preset constraints are met, solve the optimization problem online and calculate the optimal manipulated variables. The optimal manipulated variables are sent to the execution module to perform real-time, closed-loop optimization control of the moving bed temperature swing adsorption system to ensure that the system always operates in the best state.

8. The moving bed temperature swing adsorption system according to claim 7, characterized in that: The optimization objective function is specifically: ； Among them, J is the optimization objective function value, is the carbon capture weight, is the pollutant purification weight, is the external operation energy consumption weight; is the capture rate; The concentration of organic pollutants at the outlet of the purified flue gas of the multi-temperature zone moving bed reactor; is the external energy cost; The preset constraints specifically include: the adsorbent circulation rate is within the preset rate range, the adsorbent circulation rate change rate does not exceed the preset change rate threshold, the standby heat source power is within the preset power range, the temperature of the key points of each temperature zone is within the preset temperature range, the pressure drop of the multi-temperature zone moving bed reactor does not exceed the preset pressure drop threshold, the CO2 capture rate is not less than the preset capture rate threshold, and the pollutant emission concentration does not exceed the preset concentration threshold.

9. The moving bed temperature swing adsorption system according to claim 7, characterized in that: The dynamic kinetic model includes the gas phase mass balance equation for describing the mass transfer of the gas phase in the multi-temperature zone moving bed reactor, the solid phase mass balance equation for describing the mass transfer of the solid phase in the multi-temperature zone moving bed reactor, the linear driving force model for describing the adsorption of CO2 in the multi-temperature zone moving bed reactor, the Langmuir-Hinshelwood model for describing the oxidation of organic pollutants in the multi-temperature zone moving bed reactor, the gas phase heat balance equation for describing the temperature management of the gas phase in the multi-temperature zone moving bed reactor, and the solid phase heat balance equation for describing the temperature management of the solid phase in the multi-temperature zone moving bed reactor; Among them, the gas phase mass balance equation is specifically: ； in, is the concentration of component i in the gas phase; is the gas phase flow rate; is the gas phase axial backmixing coefficient; is the external diffusion mass transfer coefficient; is the specific surface area; is the gas phase concentration on the surface of the composite adsorbent particles; z represents the axial coordinate of the multi-temperature zone moving bed reactor; g is the gas phase; Among them, the solid phase mass balance equation is specifically: ； in, is the adsorption amount of component i in the solid phase; is the back-mixing coefficient of the solid phase in the axial direction; is the solid phase migration rate; is the generation / consumption rate term of component i; s is the solid phase; The linear driving force model is specifically: ； in, is the adsorption rate of CO2; is the total mass transfer coefficient in the linear driving force model; is the equilibrium adsorption capacity of CO2; is the current adsorption amount of CO2; The Langmuir-Hinshelwood model is specifically: ； in, is the catalytic oxidation rate of organic pollutants; is the catalytic reaction rate constant; is the adsorption constant of organic pollutants; is the concentration of organic pollutants in the gas phase; is the adsorption constant of oxygen; is the concentration of oxygen in the gas phase; The gas phase heat balance equation is specifically: ； in, is the gas phase void ratio; is the gas phase density; is the relative heat capacity of gas; is the thermal conductivity of the gas phase; is the gas phase superficial velocity; is the solid-gas heat transfer coefficient; is the specific surface area; is the gas phase temperature; is the solidus temperature; The solid phase heat balance equation is specifically: ； in, is the solid phase density; is the solid specific heat capacity; is the thermal conductivity of the solid phase; is the solid phase migration rate; is the solid-gas heat transfer coefficient; is the reaction enthalpy change of the j-th reaction process; is the reaction rate of the jth reaction process; is the heat transfer term from the external heat source.

10. A moving bed temperature swing adsorption method, characterized in that: A moving bed temperature swing adsorption system based on any one of claims 1 to 9, applied to the coordinated purification and carbon capture of aluminum anode baking flue gas, comprising: The composite adsorbent particles are continuously added from the top of the multi-temperature zone moving bed reactor, and the composite adsorbent particles move from top to bottom under the action of gravity, passing through the low-temperature adsorption zone, the medium-temperature catalytic adsorption zone and the high-temperature desorption and regeneration zone in sequence; The flue gas treatment flow path introduces the aluminum anode baking flue gas from the lower part of the multi-temperature zone moving bed reactor, so that the aluminum anode baking flue gas contacts with the composite adsorbent particles in countercurrent flow and flows from bottom to top; In the low-temperature adsorption zone, CO2 in the flue gas from the aluminum anode baking is adsorbed on the composite adsorbent particles; In the medium-temperature catalytic adsorption zone, organic pollutants in the flue gas from aluminum anode baking are catalytically oxidized under the action of the catalytic components of the composite adsorbent particles, while achieving stable adsorption of acidic gases in the flue gas from aluminum anode baking; The composite adsorbent particles carrying the adsorbed components enter the high-temperature decomposition and regeneration zone, and use the external heat source or the direct high-temperature waste heat of the roasting furnace to desorb the adsorbed CO2, and the CO2 product gas outlet pipeline will lead out the generated CO2 product gas; The high-temperature composite adsorbent particles after regeneration in the composite adsorbent circulation loop are discharged from the bottom of the multi-temperature zone moving bed reactor and circulated back to the top of the multi-temperature zone moving bed reactor to achieve continuous closed-loop operation; The central control unit obtains the state parameters of the multi-temperature zone moving bed reactor, composite adsorbent circulation loop, flue gas treatment flow path, and CO2 product gas outlet pipeline, and performs global optimization control based on the state parameters.

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