Mineralization reactor and mineralization reaction method for absorption and mineralization integrated technology

Abstract

The invention relates to a mineralization reactor and a mineralization reaction method for an absorption and mineralization integrated technology. A solid waste material inlet and a solid product outlet are formed in the two ends of the horizontal reactor body, and a solid-liquid mixing cavity, a reaction cavity, a flow guide buffer channel and a settling separation cavity are sequentially arranged in the horizontal reactor body between the solid waste material inlet and the solid product outlet in the conveying direction; the horizontal reactor body is further provided with a carbon dioxide rich liquid feeding port communicated with the solid-liquid mixing cavity, a solid-liquid mixing propeller is arranged in the solid-liquid mixing cavity, a reaction stirring paddle is arranged in the reaction cavity, a low-speed spiral propeller is arranged in the flow guide buffer channel, and at least two layers of modular staggered settlement plate structures are arranged in the settlement separation cavity. The reaction mineralization and regeneration of carbon dioxide rich liquor and solid waste slurry can be continuously realized, the gas-liquid mass transfer rate and the carbonate generation rate are improved, the energy consumption is reduced, the post-treatment process is simplified, and the device has the advantages of high mass transfer efficiency, full solid-liquid coupling, controllable reaction retention, efficient sedimentation and the like.

Description

Technical Field

[0001] This application relates to the field of carbon capture and resource utilization, and in particular to mineralization reactors and mineralization reaction methods for integrated absorption and mineralization technology. Background Technology

[0002] With technological advancements, carbon dioxide capture, utilization, and storage (CCUS) technology has become a crucial direction for emission reduction in the energy, metallurgical, and chemical industries. Existing chemical absorption methods, such as MEA and MDEA systems, while highly efficient at capturing carbon dioxide, suffer from high energy consumption and significant absorbent loss during regeneration. Separate mineralization methods, such as the mineralization of steel slag and carbide slag, are limited by slow reaction kinetics and low Ca content. 2+ and Mg 2+ Insufficient dissolution and difficulties in solid-liquid separation are problems. Therefore, how to organically couple the absorption and mineralization processes to construct a closed-loop system of "absorption-mineralization-regeneration" is at the forefront of current carbon dioxide emission reduction technology research. The integrated absorption-mineralization technology (IAM) developed from this is considered to be the most promising carbon capture technology at present.

[0003] However, for integrated mineralization technology, there are still several key technological bottlenecks in scaling up the mineralization reaction from the laboratory to industrial continuous equipment:

[0004] (1) Ca in solid waste 2+ / Mg 2+ The dissolution rate is slow, the residence time of the slurry in the reactor is insufficient, and the mineralization rate is low.

[0005] (2) High solids load or high viscosity slurry system has poor fluidity and is prone to sedimentation, scaling and clogging, which affects mass transfer efficiency and stable equipment operation;

[0006] (3) The solid-liquid separation of mineral products is difficult, the product has a high water content and the recovery of clarified liquid is difficult. Existing sedimentation or filtration devices are complex in structure, occupy a large area and consume a lot of energy.

[0007] (4) Most reactors are arranged vertically, such as spray towers, bubble towers, and stirred tanks, which are not suitable for continuous feeding and discharging operations with high solid loads, and it is difficult to balance long residence time reaction and efficient separation.

[0008] Traditional absorption-mineralization devices, such as vertical spray towers and bubble towers, are batch reactors that generally suffer from problems such as short residence time, low mass transfer efficiency, difficulty in solid-liquid separation, insufficient continuous operation capability, and poor adaptability. Especially in the IAM system, the reaction between carbon dioxide-rich liquid and calcium-containing solid waste produces a large amount of fine-particle carbonate, which easily leads to reactor blockage and turbulent flow field. At the same time, it requires external sedimentation or filtration devices, making the system complex and energy-intensive. Summary of the Invention

[0009] Therefore, it is necessary to provide a mineralization reactor and mineralization reaction method for integrated absorption and mineralization technology to overcome the problems of low mass transfer efficiency, difficulty in solid-liquid separation and insufficient continuous operation capability in existing carbon dioxide mineralization devices.

[0010] One embodiment of this application is a mineralization reactor for an integrated absorption and mineralization technology, which includes a horizontal reactor body;

[0011] The horizontal reactor body is provided with a solid waste inlet and a solid product outlet at both ends, and between the solid waste inlet and the solid product outlet, along the conveying direction, the interior of the horizontal reactor body is provided with a solid-liquid mixing chamber, a reaction chamber, a flow guide buffer channel and a sedimentation separation chamber in sequence.

[0012] The horizontal reactor body is also provided with a carbon dioxide rich liquid inlet that connects to the solid-liquid mixing chamber, and a solid-liquid mixing propeller is provided in the solid-liquid mixing chamber. A reaction stirring paddle is provided in the reaction chamber. A low-speed spiral propeller is provided in the flow guide buffer channel. At least two layers of modular staggered settling plate structure are provided in the settling separation chamber.

[0013] The reaction stirring paddle is a coaxial spiral propulsion stirring structure.

[0014] The mineralization reactor used in the aforementioned integrated absorption and mineralization technology employs a horizontal reactor body with a solid-liquid mixing chamber, a reaction chamber, a flow buffer channel, and a sedimentation separation chamber. On one hand, it integrates the reaction, mixing, and separation processes into a single device, enabling continuous reaction mineralization and regeneration of carbon dioxide-rich liquid and solid waste slurry. This significantly improves the gas-liquid mass transfer rate and carbonate formation rate, reduces energy consumption, and simplifies post-processing. It boasts advantages such as high mass transfer efficiency, full solid-liquid coupling, controllable reaction residence, and efficient sedimentation. On the other hand, the combination of a solid-liquid mixing propeller and a coaxial spiral propulsion stirring structure achieves continuous slurry transport and enhanced mixing. A dynamic flow field of propulsion, reflux, and remixing is formed within the reaction chamber, ensuring uniform axial and radial contact between the carbon dioxide-rich liquid and the calcium- and magnesium-containing solid waste. This significantly improves the dissolution rate of calcium and magnesium ions and their reaction rate with carbon dioxide mineralization, allowing the calcium- and magnesium-containing solid waste slurry to maintain a stable propulsion flow field even under high solid content conditions, preventing sedimentation and blockage. This technology facilitates continuous slag discharge, thereby ensuring the integrated and continuous operation of the mineralization reaction and absorbent regeneration processes. Furthermore, the flow-guiding buffer channel, combined with the modularly staggered settling plate structure in the settling separation chamber, achieves a smooth transition and wide-range uniform distribution of slurry flow velocity, avoiding short-circuiting, turbulence, and dead zones in the settling area. This enables graded settling of mineralized products and automatic reflux of clarified liquid, allowing the solid-liquid separation process to achieve a gradient evolution of sliding, slow settling, and clarification, resulting in high separation efficiency and resistance to clogging. Moreover, compared to traditional intermittent reaction devices such as vertical spray towers and bubble towers, the mineralization reactor used in the integrated absorption and mineralization technology described in this application has significant advantages such as compact structure, controllable flow field, continuous operation, high separation efficiency, and excellent anti-clogging performance. It can operate stably in high-solid-content systems with a high solid-liquid ratio, facilitating the integrated and continuous operation of carbon dioxide absorption, mineralization reaction, and absorbent regeneration separation processes, thus providing equipment support for the industrialization of carbon dioxide capture, utilization, and storage.

[0015] As an example, in the direction of gravity during use, the bottom of the flow guide buffer channel is provided with an inverted conical funnel outlet. As an example, in the direction of gravity during use, the bottom of the sedimentation separation chamber is also provided with an inverted conical funnel outlet.

[0016] In some embodiments, the settling plate structure includes a first settling plate, a second settling plate, and a third settling plate, wherein the first settling plate is located between the flow guide buffer channel and the second settling plate, and the third settling plate is located between the second settling plate and the solid product outlet.

[0017] As an example, each settling plate is a progressively raised functional protrusion structure used to achieve dynamic matching of flow regime and particle distribution during solid-liquid staged settling.

[0018] In some embodiments, in the direction of gravity during use, the horizontal reactor body is provided with a spiral slag discharger at the bottom of the settling and separation chamber. The spiral slag discharger is used to continuously discharge mineralized solids through the solid product outlet under the drive of a spiral propulsion motor.

[0019] In some embodiments, the mineralization reactor for the integrated absorption and mineralization technology further includes the screw propulsion motor, the output end of which passes through the solid product outlet and drives the screw slag discharger.

[0020] In some embodiments, the blades of the solid-liquid mixing propeller are provided with regularly arranged circular holes and radial pins to achieve dispersion of solid particles and uniform mixing of the slurry.

[0021] In some embodiments, in the direction of gravity during use, the horizontal reactor body has a regenerated liquid overflow port in the middle of the settling and separation chamber, and an overflow weir and / or filter is provided at the regenerated liquid overflow port for recovering liquid through the regenerated liquid overflow port for recycling; or,

[0022] The horizontal reactor body is equipped with a solid material propeller in the solid-liquid mixing chamber, or with a solid material propeller between the solid waste inlet and the solid-liquid mixing chamber; or...

[0023] The horizontal reactor body is provided with a solid-liquid separation viewing window at the solid-liquid mixing chamber or the sedimentation separation chamber; or...

[0024] The horizontal reactor body is provided with a heating jacket outside the reaction chamber or outside the horizontal reactor body; or,

[0025] The horizontal reactor body is equipped with detachable end caps at both ends.

[0026] In some embodiments, the solid-liquid mixing propeller, the reaction stirring impeller, and the low-speed propeller are arranged coaxially.

[0027] In some embodiments, the mineralization reactor used in the integrated absorption and mineralization technology further includes a main helical drive motor, the output end of which passes through the solid waste inlet and is integrally driven by the solid-liquid mixing propeller, the reaction stirring paddle, and the low-speed helical propeller.

[0028] In some embodiments, the mineralization reactor used in the integrated absorption and mineralization technology further includes an automated monitoring and control system, which is equipped with a control module, a level gauge, a density meter, a turbidity sensor, and a PLC control unit.

[0029] The level gauge, the density meter, and the turbidity sensor are respectively disposed in the sedimentation separation chamber, and the PLC control unit is connected to the level gauge, the density meter, and the turbidity sensor respectively.

[0030] The control module is connected to the solid-liquid mixing propeller, the reaction stirring paddle, and the low-speed propeller, respectively.

[0031] In an embodiment with the main helical drive motor, as an example, the control module is connected to the main helical drive motor and is used to control the solid-liquid mixing propeller, the reaction stirring paddle, and the low-speed helical propeller via the main helical drive motor. In an embodiment with the helical propulsion motor, as an example, the control module is connected to the helical propulsion motor and is used to control the helical propulsion motor to drive the helical slag discharger in the settling separation chamber to rotate.

[0032] In some embodiments, a mineralization reaction method for an integrated absorption and mineralization technology employs a mineralization reactor as described in any embodiment, and the mineralization reaction method for the integrated absorption and mineralization technology includes the following steps:

[0033] The pretreated calcium- and magnesium-containing solid waste enters the solid-liquid mixing chamber through the solid waste inlet;

[0034] Carbon dioxide-rich solution enters the solid-liquid mixing chamber through the carbon dioxide-rich solution inlet.

[0035] The propeller blades of the solid-liquid mixing propeller have regularly arranged circular holes and radial pins. After mixing calcium-magnesium solid waste with carbon dioxide-rich liquid in the solid-liquid mixing chamber, a slurry is formed and sent into the reaction chamber.

[0036] Within a preset temperature range, after the carbon dioxide mineralization reaction is carried out in the reaction chamber using a coaxial spiral stirring structure, the slurry after the reaction is sent into the guide buffer channel.

[0037] The reacted slurry is evenly distributed into the sedimentation and separation chamber through the flow guide buffer channel;

[0038] The reacted slurry settles in stages in the settling and separation chamber, and the mineralized solid products in the bottom slag collection zone are discharged through a spiral slag discharger. Attached Figure Description

[0039] To more clearly illustrate the technical solutions in the embodiments of this application or the conventional technology, the drawings used in the description of the embodiments or the conventional technology will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0040] Figure 1 This is a schematic diagram of a mineralization reactor used in an embodiment of the integrated absorption and mineralization technology described in this application.

[0041] Figure 2 for Figure 1 Another schematic diagram of the embodiment shown.

[0042] Figure 3 for Figure 1 A schematic diagram of the solid-liquid hybrid propeller of the embodiment shown.

[0043] Figure 4 for Figure 3 The diagram shows the function of the coaxial helical propulsion blades in the embodiment shown.

[0044] Figure 5 for Figure 1 A schematic diagram of the settlement plate structure in the embodiment shown.

[0045] Figure 6 for Figure 5 Another schematic diagram of the embodiment shown.

[0046] Reference numerals: 1. Solid waste inlet; 2. Carbon dioxide-rich liquid inlet; 3. Solid material screw propeller; 4. Solid-liquid mixing chamber; 5. Solid-liquid mixing propeller; 6. Reaction chamber; 7. Reaction stirring paddle; 8. Sedimentation chamber; 9. Guide channel; 10. First settling plate; 11. Second settling plate; 12. Third settling plate; 13. Regenerated liquid overflow outlet; 14. Solid-liquid separation viewing window; 15. Solid product outlet; 16. Screw propulsion motor; 17. Main screw drive motor; 18. Low-speed screw propeller; 19. Conveying direction; 20. Slag collection area. Detailed Implementation

[0047] To make the above-mentioned objectives, features, and advantages of this application more apparent and understandable, the specific embodiments of this application are described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of this application. However, this application can be implemented in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of this application. Therefore, this application is not limited to the specific embodiments disclosed below.

[0048] It should be noted that when a component is referred to as being "fixed to" or "set on" another component, it can be directly on the other component or there may be an intermediate component. When a component is considered to be "connected to" another component, it can be directly connected to the other component or there may be an intermediate component present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and similar expressions used in this application's specification are for illustrative purposes only and do not represent the only possible implementation.

[0049] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, "multiple" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0050] In this application, unless otherwise expressly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature and the second feature are in indirect contact through an intermediate medium. Furthermore, "above," "over," and "on top" the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0051] Unless otherwise defined, all technical and scientific terms used in this application have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used in this application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. The term "and or" as used in this application includes any and all combinations of one or more of the associated listed items.

[0052] To overcome the problems of low mass transfer efficiency, difficult solid-liquid separation, and insufficient continuous operation capacity in traditional carbon dioxide mineralization devices, this application discloses a mineralization reactor and mineralization reaction method for integrated absorption and mineralization technology, which includes some or all of the technical features of the following embodiments. In one embodiment of this application, a mineralization reactor for integrated absorption and mineralization technology is as follows: Figure 1 and Figure 2As shown, it includes a horizontal reactor body; the two ends of the horizontal reactor body are respectively provided with a solid waste inlet 1 and a solid product outlet 15, and between the solid waste inlet 1 and the solid product outlet 15, along the conveying direction 19, the interior of the horizontal reactor body is sequentially provided with a solid-liquid mixing chamber 4, a reaction chamber 6, a flow guide buffer channel 9 and a sedimentation separation chamber 8; the horizontal reactor body is also provided with a carbon dioxide rich liquid inlet 2 connected to the solid-liquid mixing chamber 4, and a solid-liquid mixing propeller 5 is provided in the solid-liquid mixing chamber 4, a reaction stirring paddle 7 is provided in the reaction chamber 6, a low-speed spiral propeller 18 is provided in the flow guide buffer channel 9, and a sedimentation separation chamber 8 is provided with at least two layers of modular staggered sedimentation plate structures; wherein, the reaction stirring paddle 7 is a forward and reverse coaxial spiral propulsion stirring structure.

[0053] This design, employing a horizontal reactor body with a solid-liquid mixing chamber 4, a reaction chamber 6, a flow-guiding buffer channel 9, and a settling and separation chamber 8, integrates the reaction, mixing, and separation processes into a single device. This allows for continuous reaction mineralization and regeneration of carbon dioxide-rich liquid and solid waste slurry, significantly improving gas-liquid mass transfer rate and carbonate formation rate, reducing energy consumption, and simplifying post-processing. It offers advantages such as high mass transfer efficiency, full solid-liquid coupling, controllable reaction residence, and efficient settling. Furthermore, the solid-liquid mixing propeller 5, combined with a coaxial spiral propulsion and stirring structure, enables continuous slurry transport and enhanced mixing. A dynamic flow field of propulsion, reflux, and remixing is formed within the reaction chamber 6, ensuring uniform axial and radial contact between the carbon dioxide-rich liquid and the calcium- and magnesium-containing solid waste. This significantly improves the dissolution rate of calcium and magnesium ions and their mineralization reaction rate with carbon dioxide. Consequently, the calcium- and magnesium-containing solid waste slurry can maintain a stable propulsion flow field even under high solid content conditions, preventing sedimentation and clogging, which is beneficial for the preparation of... The integrated absorption and mineralization technology described in this application achieves continuous slag discharge, thereby ensuring the integrated and continuous operation of the mineralization reaction and absorbent regeneration process. Furthermore, the flow guide buffer channel 9, combined with the modularly staggered settling plate structure in the settling separation chamber 8, achieves a smooth transition and wide-range uniform distribution of slurry flow velocity, avoiding short-circuiting, turbulence, and dead zones in the settling zone. This enables graded settling of mineralized products and automatic reflux of clarified liquid, allowing the solid-liquid separation process to achieve a gradient evolution of sliding, slow settling, and clarification, resulting in high separation efficiency and resistance to clogging. Moreover, compared to traditional intermittent reaction devices such as vertical spray towers and bubble towers, the mineralization reactor used in this application has significant advantages such as compact structure, controllable flow field, continuous operation, high separation efficiency, and excellent anti-clogging performance. It can operate stably in systems with high solid content and solid-liquid ratios, facilitating the integrated and continuous operation of carbon dioxide absorption, mineralization reaction, and absorbent regeneration separation processes, thus providing equipment support for the industrialization of carbon dioxide capture, utilization, and storage.

[0054] In some embodiments, a mineralization reaction method for an integrated absorption and mineralization technology employs the mineralization reactor described in any embodiment. The method includes the following steps: pretreated calcium-magnesium-containing solid waste enters a solid-liquid mixing chamber 4 through a solid waste inlet 1; carbon dioxide-rich liquid enters the solid-liquid mixing chamber 4 through a carbon dioxide-rich liquid inlet 2; using regularly arranged circular holes and radial pins on the blades of a solid-liquid mixing propeller 5, the calcium-magnesium-containing solid waste and the carbon dioxide-rich liquid are mixed in the solid-liquid mixing chamber 4 to form a slurry, which is then fed into a reaction chamber 6; within a preset temperature range, a coaxial spiral propulsion stirring structure is used in the reaction chamber 6 to perform a carbon dioxide mineralization reaction, and the reacted slurry is then fed into a flow guide buffer channel 9; the reacted slurry is evenly distributed to a settling and separation chamber 8 through the flow guide buffer channel 9; the reacted slurry undergoes graded settling in the settling and separation chamber 8, and the mineralized solid products in the bottom slag collection area 20 are discharged through a spiral slag discharger. It is understood that, since the mineralization reactor used in the integrated absorption and mineralization technology of any embodiment is adopted, the mineralization reaction method used in the integrated absorption and mineralization technology also has the beneficial technical effects of the mineralization reactor used in the integrated absorption and mineralization technology, which will not be elaborated here.

[0055] This design, on the one hand, achieves integrated and continuous operation of the mineralization reaction and absorbent regeneration process through deep coupling of structure and technology. The mineralization reactor used in the integrated absorption and mineralization technology adopts a horizontal modular design, equipped with a solid-liquid mixing propeller 5 and a forward and reverse coaxial spiral propulsion stirring structure, so that the calcium-magnesium-containing solid waste slurry can still form a stable propulsion flow field under high solid content conditions, avoiding sedimentation and blockage. At the same time, at least two layers of progressively higher functional convex settling groups are integrated at the tail of the reactor to realize the graded settling of mineralization products and automatic reflux of clarified liquid. On the other hand, by integrating the reaction, mixing and separation processes into the same equipment, the coupled mineralization and regeneration of carbon dioxide-rich liquid and solid waste slurry can be continuously realized, significantly improving the gas-liquid mass transfer rate and carbonate formation rate, reducing energy consumption and simplifying the post-processing process. This provides an efficient and feasible equipment solution for the industrial promotion of the closed-loop system of absorption-mineralization-regeneration of alkaline solid wastes such as steel slag, carbide slag, and fly ash. On the other hand, through a horizontal continuous flow structure, enhanced positive and negative coaxial spiral stirring, and a three-layer gradually rising settling plate separation system, the system achieves efficient mineralization reaction and automatic solid-liquid separation of carbon dioxide-rich liquid and solid waste powder. It features thorough mixing, high reaction rate, high separation efficiency, low energy consumption, and stable operation. It can operate continuously and is suitable for carbon capture and resource utilization in the steel, calcium carbide, chemical, and building materials industries.

[0056] To ensure the highest possible reaction efficiency, the solid waste is preferably pretreated by crushing, grinding, and sieving to ensure that its particle size D90 is no greater than 150 μm and contains 10 wt.% to 60 wt.% of reactive alkaline oxide components, mainly CaO and MgO. The carbon dioxide-rich solution is a regenerated amine solution or carbonate solution that has absorbed and enriched carbon dioxide. The regenerated amine solution may be MDEA, AMP, MEA, etc., and the carbonate solution may be Na2CO3, K2CO3, etc., with a carbon dioxide loading of 0.2 mol / mol to 0.5 mol / mol to balance reaction rate and flowability.

[0057] This design, on the one hand, pre-treats solid waste to particle size limits through crushing, grinding, and screening, and combines it with weight-limited reactive alkaline oxide components to significantly increase specific surface area and substrate abundance, accelerating the dissolution of calcium and magnesium ions; on the other hand, the molar loading of carbon dioxide-rich liquid balances reactivity and flow characteristics, and works in conjunction with the solid-liquid mixing propeller 5 and the forward and reverse coaxial spiral propulsion stirring structure 7 to enhance three-phase mass transfer efficiency, avoid flow stagnation in high solid content systems, ensure the stability of the dynamic flow field within the reaction chamber 6, further improve the carbonate formation rate, facilitate continuous operation of integrated absorption and mineralization, and reduce operating energy consumption and blockage risk.

[0058] The mineralization reactor used in the integrated absorption and mineralization technology adopts a horizontal reactor body design, and therefore can also be called a horizontal continuous mineralization reactor. As an example, the horizontal reactor body is a sealed cylinder with an inner diameter of 0.8m to 2.0m and a length of 6m to 20m. In various embodiments, the horizontal reactor body has a solid waste inlet 1 and a solid product outlet 15 at both ends, respectively. This can also be understood as the solid waste inlet 1 and solid product outlet 15 being located near both ends of the horizontal reactor body. Furthermore, the specific positions of the solid waste inlet 1 and solid product outlet 15 can be flexibly set or adjusted according to production needs. The solid waste inlet 1 is used to input solid waste into the horizontal reactor body. Solid waste is typically rich in calcium and magnesium ions, and therefore can also be called calcium-magnesium-containing solid waste. It is understood that in the various embodiments of this application, "rich" and "rich liquid" are relatively abundant concepts. For example, in solid waste, the calcium ion content of carbide slag is higher than 45% by mass; and in carbon dioxide rich liquid, the molar ratio of carbon dioxide is higher than 5% or more.

[0059] This design offers several advantages. First, the horizontal sealed cylinder structure, combined with a suitable inner diameter and corresponding length, provides ample axial reaction space while ensuring the equipment's compact structure, adapting to the space requirements of continuous production. The sealing design effectively prevents carbon dioxide leakage, maintaining the stability of the reaction system. Second, the solid waste inlet 1 and solid product outlet 15 are located close to both ends and can be flexibly adjusted, precisely matching the conveying path of calcium- and magnesium-containing solid waste. This works in conjunction with the solid-liquid mixing propeller 5, the forward and reverse coaxial spiral propulsion stirring structure 7, and the low-speed spiral propeller 18 to ensure continuous material flow from feeding to reaction and then to slag discharge, avoiding localized accumulation. Third, the horizontal layout allows for a more rational axial arrangement of the solid-liquid mixing chamber 4, reaction chamber 6, flow guide buffer channel 9, and sedimentation separation chamber 8. Under the combined action of gravity and propulsion, the material flows smoothly through each functional area. Combined with the modular staggered sedimentation plate structure of the sedimentation separation chamber 8, this further optimizes the flow field distribution, reduces short-circuiting and dead zones, and is more conducive to the stable operation of high-solids-content systems.

[0060] In each embodiment, between the solid waste inlet 1 and the solid product outlet 15, along the conveying direction 19, the interior of the horizontal reactor body is sequentially provided with a solid-liquid mixing chamber 4, a reaction chamber 6, a flow guide buffer channel 9, and a sedimentation separation chamber 8. As an example, the solid-liquid mixing chamber 4 is used to mix solid waste with carbon dioxide-rich liquid so that calcium and magnesium ions in the solid waste can fully contact the carbon dioxide-rich liquid. The reaction chamber 6 is used to provide reaction space and reaction heat energy, and to accommodate the mixed slurry for a sufficient reaction time. The flow guide buffer channel 9 is used to evenly distribute the reacted slurry to the sedimentation separation chamber 8. The sedimentation separation chamber 8 stages and settles the reacted slurry, and discharges the mineralized solid product from the bottom.

[0061] This design, on the one hand, with the solid-liquid mixing chamber 4, reaction chamber 6, flow guide buffer channel 9, and sedimentation separation chamber 8 arranged sequentially along the conveying direction 19, achieves a seamless process of mixing, reaction, buffering, and separation, eliminating the need for additional transfer devices, significantly simplifying the system architecture and reducing transfer energy consumption; on the other hand, the solid-liquid mixing chamber 4 focuses on the premixing of calcium- and magnesium-containing solid waste with carbon dioxide-rich liquid, and works with the solid-liquid mixing propeller 5 to achieve full contact, laying a solid foundation for the efficient dissolution of calcium and magnesium ions. The reaction chamber 6 provides sufficient reaction space and heat energy, and works in conjunction with the forward and reverse coaxial propellers. The mixing structure 7 ensures that the mixed slurry has sufficient reaction residence time, significantly improving the mineralization reaction rate and conversion rate. On the other hand, the guide buffer channel 9 uses a low-speed screw propeller 18 to smoothly transport the slurry, avoiding turbulent impact and ensuring uniform distribution to the settling separation chamber 8. The staged settling function of the settling separation chamber 8, together with the modular staggered settling plate structure, realizes rapid separation and bottom discharge of mineralized solid products, which is highly compatible with the solid product outlet 15. There is no material retention throughout the process, and the anti-clogging performance is excellent, effectively ensuring the stability and efficiency of integrated continuous operation.

[0062] To facilitate the maintenance of the internal structural components of the horizontal reactor body, in some embodiments, the two ends of the horizontal reactor body are respectively provided with detachable end caps. For example, when the detachable end caps are open, the internal structural components of the horizontal reactor body can be cleaned, maintained, or replaced; when the detachable end caps are closed, they seal both ends of the horizontal reactor body. This design, on the one hand, allows for convenient cleaning, maintenance, or replacement of internal structural components such as the solid-liquid mixing propeller 5, the forward and reverse coaxial helical propulsion stirring structure 7, the low-speed helical propeller 18, and the modular staggered settling plate when the detachable end caps are open, significantly reducing maintenance difficulty and downtime; on the other hand, when closed, it can tightly seal both ends of the horizontal reactor body, thereby ensuring the sealing of the reaction system, preventing carbon dioxide leakage and material spillage, and maintaining stable operating conditions in areas such as the reaction chamber 6; furthermore, the flexible disassembly and assembly characteristics balance equipment maintenance convenience and operational sealing, effectively reducing operation and maintenance costs and improving the long-term reliability of the equipment.

[0063] In each embodiment, the horizontal reactor body is further provided with a carbon dioxide-rich liquid inlet 2 connected to the solid-liquid mixing chamber 4, and a solid-liquid mixing propeller 5 is provided in the solid-liquid mixing chamber 4. The solid waste and carbon dioxide-rich liquid are mixed by the solid-liquid mixing propeller 5 to form a slurry, which is then fed into the reaction chamber 6. In order to ensure the reaction balance as much as possible, the feeding rates of the calcium-magnesium-containing solid waste input from the solid waste inlet 1 and the carbon dioxide-rich liquid input from the carbon dioxide-rich liquid inlet 2 are controlled. As an example, the solid-liquid feeding rate is controlled by frequency conversion, and the solid-liquid ratio of the system is controlled between 50 g / L and 150 g / L to ensure the balance between slurry fluidity and reaction efficiency.

[0064] This design achieves several advantages. First, the carbon dioxide-rich liquid inlet 2 precisely connects to the solid-liquid mixing chamber 4, allowing the solid-liquid mixing propeller 5 to quickly agitate the calcium-magnesium-containing solid waste and the carbon dioxide-rich liquid into a uniform slurry. This maximizes the contact area between the two, laying a solid foundation for the efficient dissolution of calcium and magnesium ions and subsequent mineralization reactions. Second, the frequency-controlled feed rate design allows for flexible adjustment of the solid-liquid ratio. This avoids both excessively high solid-liquid ratios that could lead to slurry viscosity and blockage of the solid-liquid mixing chamber 4 or the flow buffer channel 9, and excessively low solid-liquid ratios that could reduce reaction efficiency. This, combined with the coaxial spiral propulsion stirring structure 7 in the reaction chamber 6, maintains a stable dynamic flow field within the chamber. Third, the precise matching of feed and reaction ensures that the slurry maintains good fluidity and reactivity as it flows through various functional areas, effectively improving the mineralization reaction conversion rate and equipment operational stability, thereby reducing the probability of downtime due to malfunctions.

[0065] To facilitate observation of the internal state of the solid-liquid mixing chamber 4, in some embodiments, the horizontal reactor body is provided with a solid-liquid separation viewing window 14 at the solid-liquid mixing chamber 4, so that the user can observe the internal state of the solid-liquid mixing chamber 4 through the solid-liquid separation viewing window 14 during the mixing or production process. As an example, the solid-liquid separation viewing window 14 is used to monitor the sedimentation and separation state of solid waste and carbon dioxide-rich liquid in real time; since the reaction chamber 6 usually needs to be heated to provide reaction heat energy and is prone to generating water mist, the solid-liquid separation viewing window 14 is not set in the reaction chamber 6 to avoid affecting the reaction effect and observation effect.

[0066] To facilitate the better delivery of solid waste into the solid-liquid mixing chamber 4, in some embodiments, the horizontal reactor body is provided with a solid material propeller 3 in the solid-liquid mixing chamber 4, or a solid material propeller 3 is provided between the solid waste inlet 1 and the solid-liquid mixing chamber 4; considering that the solid material propeller 3 pushes solid waste, while the solid-liquid mixing propeller 5 pushes solid-liquid slurry, i.e., slurry, as an example, the torque of the solid material propeller 3 is greater than the torque of the solid-liquid mixing propeller 5.

[0067] This design has several advantages. First, the solid material propeller 3 is installed inside the solid-liquid mixing chamber 4 or between the solid waste inlet 1 and the solid-liquid mixing chamber 4, precisely connecting the solid material conveying path. Its greater torque is adapted to the solid characteristics of calcium- and magnesium-containing solid waste, and it can powerfully push the material, avoiding accumulation and blockage in the feeding section and ensuring continuous and smooth feeding. Second, it can form a functional division and synergy with the solid-liquid mixing propeller 5. The former focuses on the efficient conveying of solid waste, while the latter is responsible for the full mixing of solid and liquid into a slurry. The two steps are seamlessly connected, greatly improving the material flow and premixing efficiency. Third, with the frequency-controlled feeding rate and a suitable solid-liquid ratio, it ensures that the solid waste enters the solid-liquid mixing chamber 4 smoothly and makes precise contact with the carbon dioxide-rich liquid, which is conducive to the enhanced reaction of the forward and reverse coaxial spiral propulsion stirring structure 7 in the reaction chamber 6.

[0068] To improve the mixing uniformity of solid waste and carbon dioxide-rich liquid, in some embodiments, the blades of the solid-liquid mixing propeller 5 are provided with regularly arranged circular holes and radial pins to achieve dispersion of solid particles and uniform mixing of the slurry. As an example, the diameter of the radial pins is smaller than the diameter of the circular holes, so as to combine the jet disturbance formed through the circular holes with the shearing action of the pins, which can form multidirectional flow and local high-shear zones during material propulsion, effectively breaking up agglomerated particles and improving the uniformity of solid-liquid mixing and reaction contact efficiency.

[0069] This design, on the one hand, allows for the synergistic effect of the regular circular holes and radial pins on the blades of the solid-liquid mixing propeller 5. The circular holes generate jet disturbance, while the pins provide shear force. The combination of these two elements creates multi-directional flow and local high-shear zones, which can efficiently break up agglomerated particles of calcium- and magnesium-containing solid waste, significantly improving the uniformity of solid-liquid mixing and ensuring sufficient contact between calcium and magnesium ions and carbon dioxide-rich liquid, laying a solid foundation for rapid ion dissolution. On the other hand, the enhanced mixing effect is seamlessly integrated with the conveying function of the solid material propeller 3, ensuring that the slurry has excellent homogeneity before entering the reaction chamber 6. This, combined with the coaxial forward and reverse spiral propulsion stirring structure 7, creates a synergistic effect, significantly improving the contact efficiency and reaction rate of the mineralization reaction. Furthermore, it effectively avoids local accumulation caused by particle agglomeration, ensuring good fluidity of the slurry at a suitable solid-liquid ratio, reducing the risk of blockage in the solid-liquid mixing chamber 4 and subsequent flow channels, further ensuring the continuous and stable operation of the integrated absorption and mineralization process, and contributing to an increase in carbonate formation rate.

[0070] In each embodiment, the reaction chamber 6 is provided with a reaction stirring paddle 7; wherein, the reaction stirring paddle 7 is a coaxial spiral propulsion stirring structure; as an example, such as Figure 3 and Figure 4 As shown, the coaxial helical propulsion stirring structure has a propeller-like shape and can therefore be called a coaxial helical propulsion stirring paddle or coaxial helical propulsion blade. As an example, the reaction stirring paddle 7 includes forward helical blades and reverse helical blades with overlapping shafts. The forward helical blades are used for axial propulsion of the slurry, i.e., the material, while the reverse helical blades are used to generate local backflow to cooperate with the forward helical blades in achieving a stirring effect. This ensures that the calcium- and magnesium-containing solid waste in the slurry comes into full contact with the carbon dioxide-rich liquid, thereby improving the reaction efficiency.

[0071] As an example, the reaction chamber 6 is equipped with coaxial forward and reverse spiral propulsion blades as reaction stirring paddles 7. The forward spiral blades have a wider pitch, for example, 300mm to 500mm, and an inclination angle of 45° to 60°, for axial propulsion of materials. The main spiral drive motor 17 adopts frequency conversion speed regulation control, with a propulsion speed range of 5 rpm to 20 rpm and an axial propulsion speed of 0.02m / s to 0.08m / s, which can be adjusted according to the solid-liquid ratio and the throughput. The reverse spiral blades have a narrower pitch, for example, 150mm to 250mm, and an inclination angle of 60° to 75°, for generating local backflow. The two sets of blades are staggered on the same axis, with an axial projection overlap of 30% to 50%, forming a continuous "∞" or "8" shaped flow field in the axial section region, realizing local backflow and shear mixing of the slurry. As an example, the area ratio of the forward and reverse spiral blades is 1.5:1 to 2:1. By adjusting the area ratio, the backflow intensity and shear rate distribution can be controlled, allowing the slurry to maintain moderate backmixing while advancing axially, extending the residence time of the material in the reaction zone, and ensuring a reaction time of 1 to 2 hours, thereby improving Ca.2+ / Mg 2+ The reaction efficiency with carbon dioxide and the carbonate formation rate.

[0072] This design, on the one hand, allows the forward and reverse spiral blades of the coaxial helical propulsion mixing structure 7 to work together. The forward spiral blades, with a wide pitch and an inclination angle of 45° to 60°, ensure smooth axial propulsion of the slurry, while the reverse spiral blades, with a narrow pitch and an inclination angle of 60° to 75°, precisely generate local backflow without affecting the main thrust of the forward spiral blades. The 30% to 50% axial projection overlap forms a continuous figure-eight flow field in the axial section, enabling the slurry to complete efficient shear mixing while being propulsed axially. This completely breaks down local concentration and temperature gradients, allowing calcium- and magnesium-containing solid waste and carbon dioxide-rich liquid to fully contact each other in the radial and axial directions, significantly improving the dissolution efficiency of calcium and magnesium ions and the uniformity of the mineralization reaction. On the other hand, the variable frequency speed control design of the main spiral drive motor 17 can be flexibly adjusted according to the solid-liquid ratio and processing volume. The carefully adjusted ratio of the forward and reverse blade areas can precisely control the backflow intensity and shear rate distribution, ensuring that the high-solids-content slurry does not settle or clog, adapting to different working conditions. On the other hand, this structure effectively extends the residence time of materials in reaction chamber 6, providing sufficient time for the mineralization reaction, significantly improving ion reaction efficiency and carbonate formation rate, and creating a synergistic effect with the premixing effect of solid-liquid mixing chamber 4. Furthermore, its flow field is highly controllable and its energy consumption is lower, offering a wider range of adaptability compared to traditional stirring structures. It maintains stable reaction conditions within the sealed horizontal reactor body, ensuring reaction stability and providing core power support for the integrated continuous operation of carbon dioxide absorption, mineralization, and absorbent regeneration.

[0073] Considering that the reaction process in reaction chamber 6 requires heat energy, in some embodiments, a heating jacket is provided outside the horizontal reactor body or outside the horizontal reactor body to heat the slurry inside the reaction chamber 6. As an example, the heating jacket includes an electric heating device, or it is a heat conduction device used to access external waste heat to heat the slurry inside the reaction chamber 6, such as waste heat gas or waste hot water, to maximize energy utilization efficiency. As an example, the heating jacket outside the reaction chamber 6 is used to maintain the reaction temperature between 30°C and 60°C. The heating medium can be flexibly selected according to the industrial scenario: when the device is used in power plants, chemical plants, or steel enterprises, low-pressure steam, circulating hot water, or waste heat from flue gas can be used as the heating source. The temperature of the heat medium flowing into the jacket is controlled between 50°C and 90°C, and a closed-loop control system is formed by a temperature sensor and an automatic regulating valve to achieve constant temperature operation in the reaction zone.

[0074] This design achieves several advantages. First, the heating jacket outside the reaction chamber 6 precisely maintains an optimized reaction temperature range. This temperature is suitable for the mineralization reaction characteristics of calcium- and magnesium-containing solid waste and carbon dioxide-rich liquid, significantly accelerating the dissolution of calcium and magnesium ions and their reaction rate with carbon dioxide. Combined with the 8-shaped flow field of the coaxial spiral stirring structure 7, heat transfer and material mixing are simultaneously enhanced, avoiding differences in reaction efficiency caused by uneven local temperatures. Second, the heating jacket can flexibly use electric heating or industrial waste heat as a heat source, reducing additional energy consumption, improving energy utilization efficiency, and adapting to the supporting needs of different industrial scenarios such as power plants and chemical plants. The 50℃ to 90℃ heat medium temperature design balances heating efficiency and operational safety. Third, the closed-loop control system composed of temperature sensors and automatic regulating valves achieves precise and constant temperature control in the reaction zone, avoiding temperature fluctuations from affecting the slurry flowability and reaction balance, ensuring stable and efficient mineralization reaction.

[0075] In each embodiment, the flow-guiding buffer channel 9 is provided with a low-speed spiral propeller 18. As an example, in the gravity direction during use, the bottom of the flow-guiding buffer channel 9 is provided with an inverted conical funnel outlet. As an example, in the gravity direction during use, the bottom of the settling separation chamber 8 is also provided with an inverted conical funnel outlet. As an example, the flow-guiding buffer channel 9 stabilizes the slurry flow direction and evenly distributes the slurry into the settling separation chamber 8 through the low-speed spiral propeller 18. As an example, the low-speed spiral propeller 18 adopts a large-pitch blade structure with a blade inclination angle of 60° to 75°, and at least three, for example, four to eight, inverted conical funnel outlets are evenly distributed in the propulsion direction to achieve a wide and uniform distribution of the slurry in the settling zone and avoid the generation of local short-circuit or dead zones.

[0076] This design, on the one hand, utilizes a large-pitch blade structure and a blade inclination angle of 60° to 75° in the low-speed screw propeller 18, which can smoothly guide the slurry discharged from the reaction chamber 6, avoiding turbulence caused by sudden changes in flow velocity. Combined with the inverted conical funnel outlets at the bottom of the guide buffer channel 9 and the settling separation chamber 8, it initially guides the settling trend of solid particles, laying a solid foundation for subsequent separation. On the other hand, the evenly distributed inverted conical funnel outlets achieve uniform distribution of the slurry width, minimizing the generation of local short-circuiting and dead zones within the settling separation chamber 8, allowing the slurry to settle smoothly and efficiently with the modular components. The drop plate structure ensures full contact, significantly improving the efficiency of graded sedimentation. On the other hand, it provides stable conveying and uniform distribution functions. It supports the enhanced reaction effect of the positive and negative coaxial spiral propulsion stirring structure 7 in the reaction chamber 6 and connects to the solid-liquid separation process of the sedimentation separation chamber 8 below, forming a seamless connection between reaction-buffering-separation. It is suitable for high solid content systems, avoids solid particle accumulation and blockage, and ensures that mineralized solid products are smoothly collected through the inverted conical funnel outlet and discharged through the solid product outlet 15, further improving the continuous operation stability and separation reliability of the integrated absorption and mineralization technology.

[0077] In each embodiment, the settling separation chamber 8 is provided with at least two layers of modularly staggered settling plate structures; as an example, such as Figure 5 and Figure 6 As shown, the settling plate structure includes a three-layer modular staggered settling plate structure, that is, the three-layer modular staggered settling plate structure has three layers of settling plates, each of which is a modular settling plate, and adjacent layers of settling plates are staggered. In some embodiments, the settling plate structure includes a first settling plate 10, a second settling plate 11, and a third settling plate 12, wherein the first settling plate 10 is located between the flow guide buffer channel 9 and the second settling plate 11, and the third settling plate 12 is located between the second settling plate 11 and the solid product outlet 15. As an example, each settling plate is a gradually rising functional protrusion structure, used to achieve dynamic matching of flow pattern and particle distribution during solid-liquid classification and settling. The settling separation chamber 8 adopts a three-layer modular staggered settling plate structure, consisting of a coarse separation layer, a main settling layer, and a fine separation layer from top to bottom. Each settling plate is designed with a gradually increasing functional protrusion structure to achieve dynamic matching of flow state and particle distribution during solid-liquid graded settling, thereby significantly improving separation efficiency and anti-clogging performance.

[0078] As an example, the first settling plate 10 has an inclination angle of 55° to 65°, and several triangular guide protrusions are provided on the plate surface along the flow direction to guide large particles to slide down quickly. The height of the guide protrusions gradually increases along the water flow direction, and the extension direction of the protrusions forms a guide angle of 25° to 35° with the settling direction. Through the gradually rising guide structure of the first settling plate 10, which has a low inlet and a high outlet, a clear sliding channel is formed in the initial settling stage of the particles, allowing larger solid particles to quickly detach from the liquid flow and slide into the slag collection area under the combined action of gravity and guiding force, thereby reducing the load on the lower layer and avoiding accumulation and blockage on the plate surface.

[0079] As an example, the second settling plate 11 has an inclination angle of 50° to 60°, and its surface is provided with continuous wavy protrusions extending along the flow direction, with the wave height and wavelength gradually changing synchronously along the flow direction. Through the gradual design of the waveform geometry parameters, the second settling plate 11 can generate multi-scale micro-vortices in different flow velocity ranges. Flexible disturbances are formed at the inlet end to prevent the initial flocs from being destroyed; a dense vortex zone is formed at the outlet end to enhance the aggregation and collision settling of medium-sized particles, creating conditions for further separation of fine particles.

[0080] As an example, the third settling plate 12 has an inclination angle of 45° to 55°, and its surface is arranged with staggered lattice-like hemispherical protrusions. The height of the protrusions gradually increases along the flow direction, while the center-to-center spacing gradually decreases from upstream to downstream. The third settling plate 12 forms a dense micro-disturbance zone and deceleration zone effect at the settling end, significantly extending the settling path of fine particles, enhancing the probability of collision and interception, and achieving efficient capture of fine particles. The staggered arrangement of the lattice protrusions in this layer not only disperses the flow field but also prevents sedimentation and blockage, ensuring stable effluent clarity in the settling zone.

[0081] As an example, the settling plates are installed in a staggered modular unit configuration, with the interlayer spacing controlled between 50mm and 80mm. Each layer forms a graded buffer and flow-guiding transition zone. The coarse separation layer is responsible for rapid sliding and diversion, the main settling layer for flocculation and slow settling, and the fine separation layer for fine particle capture and final clarification. This three-layer, gradually rising design causes the settling flow field to gradually converge along the flow direction, allowing the particle trajectory to continuously evolve from sliding to slow settling to convergence, forming a dynamic gradient separation chain. This achieves a multi-stage settling effect where large particles fall first, small particles settle slowly, and fine particles are ultimately captured. During this process, solid particles in the slurry slide down gradually under the influence of gravity and the guiding convexity, and collect in the funnel-shaped slag collection area at the bottom of the settling and separation chamber 8, where they are continuously discharged by the bottom spiral slag discharger. Meanwhile, the upper clarified liquid gradually separates from bottom to top under the laminar flow guidance of the three-stage settling plates. When the liquid level reaches the set height, the liquid overflows evenly through the overflow weir on the upper right and then evenly through the regenerated liquid overflow port 13, achieving graded diversion of solids downward and liquid upward, thus completing the continuous solid-liquid separation process. This structure can achieve efficient clarification and continuous slag discharge without adding external filtration or centrifuge equipment, ensuring long-term stable operation of the system.

[0082] This design, on the one hand, uses a three-layer modular staggered settling plate structure to form a gradient separation chain of coarse separation, main settling, and fine separation. Each layer is specifically adapted to particles of different sizes. The first layer, with triangular guide protrusions at an inclination angle of 55° to 65°, guides large particles to slide down quickly, reducing the load on the lower layer. The second layer, with wave-shaped protrusions at an inclination angle of 50° to 60°, generates multi-scale micro-vortices, promoting the aggregation and settling of medium-sized particles. The third layer, with staggered lattice protrusions at an inclination angle of 45° to 55°, extends the settling path of fine particles, achieving efficient capture. The three-stage synergy significantly improves separation efficiency and stabilizes the quality of the clarified liquid. On the other hand, the progressively higher functional protrusions in each layer, combined with the interlayer spacing, allow the settling flow field to gradually converge along the flow direction. The particle trajectory completes a continuous evolution of sliding, slow descent, and aggregation. Coupled with the uniform slurry distribution of the low-speed spiral propeller 18 in the flow guide buffer channel 9, short-circuiting, turbulence, and dead zones are completely eliminated. The flow field stability is significantly better than that of traditional separation structures. At the same time, the modular staggered installation design facilitates disassembly and maintenance, and the protruding structure effectively prevents particle deposition and blockage, exhibiting excellent anti-clogging performance. Furthermore, the structural design eliminates the need for additional filtration or centrifugation equipment, enabling solid particles to be progressively collected in the funnel-shaped slag collection area at the bottom of the settling separation chamber 8. The particles are then continuously discharged through the bottom spiral slag discharger and the solid product outlet 15. The clarified liquid overflows uniformly through the regenerated liquid overflow port 13, perfectly connecting the mineralization reaction in the reaction chamber 6 with the subsequent absorbent regeneration process. This simplifies the system architecture, reduces energy consumption, and ensures the continuity and efficiency of solid-liquid separation.

[0083] In some embodiments, in the direction of gravity during use, the horizontal reactor body is provided with a spiral slag discharger at the bottom of the settling separation chamber 8. The spiral slag discharger, driven by a spiral propulsion motor 16, continuously discharges mineralized solids through the solid product outlet 15. In some embodiments, the mineralization reactor for the integrated absorption and mineralization technology further includes the spiral propulsion motor 16, the output end of which passes through the solid product outlet 15 and drives the spiral slag discharger. As an example, the bottom of the settling separation chamber 8 is provided with a spiral slag discharger to achieve continuous discharge of mineralized solids; the slag discharger can be driven by the spiral propulsion motor 16, for example, a speed-regulating motor, to control the slag discharge rate and maintain a stable liquid level in the settling zone.

[0084] This design, on the one hand, allows the spiral slag discharger, driven by the spiral propulsion motor 16, to precisely connect to the funnel-shaped slag collection area at the bottom of the settling separation chamber 8, continuously pushing the mineralized solids captured by the three-stage settling plate structure to the solid product outlet 15 for discharge, avoiding solid accumulation and clogging of the separation channel, and ensuring the continuity of the solid-liquid separation process; on the other hand, the slag discharge rate can be flexibly adjusted through the motor speed regulation, matching both the mineralization reaction generation rate and maintaining a stable liquid level in the settling separation chamber 8, ensuring the smooth overflow of the upper clarified liquid through the regenerated liquid overflow port 13, and ensuring orderly solid-liquid separation; furthermore, the continuous slag discharge characteristic design is deeply compatible with the integrated design of the horizontal reactor body, and together with the feeding and conveying of the solid material spiral propulsion paddle 3 and the reaction enhancement of the forward and reverse coaxial spiral propulsion stirring structure 7, a closed-loop continuous process of feeding-reaction-separation-slag discharge is formed, eliminating the need for shutdown for slag cleaning, reducing operation and maintenance costs, and further improving the stability and reliability of equipment operation under high solid content systems.

[0085] To reuse the clear liquid in the upper layer of sedimentation separation, in some embodiments, the horizontal reactor body has a regenerated liquid overflow port 13 in the middle of the sedimentation separation chamber 8 in the direction of gravity during use. The regenerated liquid overflow port 13 is equipped with an overflow weir and / or a filter body for recovering liquid through the regenerated liquid overflow port 13 for recycling. As an example, such as... Figure 1 or Figure 2 As shown, the sedimentation separation chamber 8 is provided with a regenerated liquid overflow port 13 in the upper right part. The front end of the regenerated liquid overflow port 13 is provided with an overflow weir for recovering the clarified liquid and returning it to the system for recycling.

[0086] This design allows for several advantages. First, the overflow port 13 of the regenerated liquid in the middle of the settling separation chamber 8, combined with an overflow weir and / or filter, accurately recovers the clear liquid from the upper layer after clarification by the three-stage settling plate structure. This effectively traps residual fine particles, ensuring the purity of the recovered liquid and preventing impurities from interfering with subsequent solid-liquid mixing and mineralization reactions. Second, the recovered liquid can be recycled back to the solid-liquid mixing chamber 4 as a reaction medium, significantly reducing the amount of carbon dioxide-rich liquid to be replenished, lowering raw material consumption and operating costs, and improving resource utilization. Third, the overflow weir design ensures a stable overflow of the clear liquid, which, combined with the continuous slag discharge of the spiral slag remover, maintains a stable liquid level in the settling separation chamber 8, ensuring orderly solid-liquid separation and deep compatibility with the integrated process.

[0087] To facilitate observation of the internal state of the settling separation chamber 8, in some embodiments, the horizontal reactor body is provided with a solid-liquid separation viewing window 14 at the settling separation chamber 8, so that users can observe the internal state of the settling separation chamber 8 through the solid-liquid separation viewing window 14 during the production process. As an example, the solid-liquid separation viewing window 14 can be used to monitor the settling layer interface, liquid level, and particle distribution in real time. This design offers several advantages. First, the solid-liquid separation viewing window 14 allows for real-time observation of the sedimentation layer interface, liquid level, and particle distribution within the sedimentation separation chamber 8. This enables users to intuitively understand the separation conditions of the three-stage sedimentation plate structure, promptly detect abnormalities such as particle accumulation and liquid level imbalance in the sedimentation separation chamber 8, and prevent the escalation of faults from affecting continuous operation. Second, it allows for internal status checks without shutdown and disassembly, significantly reducing maintenance difficulty and downtime losses. Combined with the maintenance function of the detachable end caps, it further enhances the convenience of equipment maintenance. Third, it provides a clear basis for optimizing operating parameters, assisting in precise control of slag discharge rate, feed ratio, etc., ensuring stable solid-liquid separation efficiency in the sedimentation separation chamber 8, and providing visual support for the smooth progress of the integrated absorption and mineralization process.

[0088] In some embodiments, the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18 are coaxially arranged. In some embodiments, the mineralization reactor for the integrated absorption and mineralization technology also includes a main screw drive motor 17. The output end of the main screw drive motor 17 passes through the solid waste inlet 1 and is integrally connected to the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18. That is, the output end of the main screw drive motor 17 simultaneously drives the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18 to rotate coaxially. By designing different propeller shapes and sizes, the force of the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18 can be controlled.

[0089] This design, on the one hand, simplifies the equipment's transmission structure significantly by integrating the coaxially mounted solid-liquid mixing propeller 5, reaction stirring paddle 7, and low-speed screw propeller 18 with the main screw drive motor 17. This reduces the complexity of multi-motor coordination control and potential malfunctions, lowers manufacturing costs and operating energy consumption, and allows for a more compact internal layout of the horizontal reactor body, without occupying additional space. On the other hand, the synchronous rotation of the three components creates precise working coordination. The strong mixing effect of the solid-liquid mixing propeller 5, the enhanced 8-shaped flow field reaction of the reaction stirring paddle 7, and the smooth slurry distribution function of the low-speed screw propeller 18 are seamlessly connected. The rhythm of material from premixing to reaction to buffering distribution is highly matched, avoiding local material stagnation or excessively rapid propulsion, and ensuring stable slurry flow under solid-liquid ratios. Furthermore, the differentiated design of the propeller shape and size controls the force of each component, allowing the solid-liquid mixing propeller 5 to focus on dispersion and mixing, the reaction stirring paddle 7 to focus on propulsion and reflux, and the low-speed screw propeller 18 to focus on smooth delivery. Each component performs its specific function while working synergistically to further enhance the integrated continuous process of mixing-reaction-buffering-separation.

[0090] In some embodiments, the mineralization reactor used in the integrated absorption and mineralization technology further includes an automated monitoring and control system. This system includes a control module, a level gauge, a density meter, a turbidity sensor, and a PLC control unit. The level gauge, density meter, and turbidity sensor are respectively disposed in the settling and separation chamber 8. The PLC control unit is connected to the level gauge, density meter, and turbidity sensor. The control module is connected to the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18. In an embodiment with a main screw drive motor 17, for example, the control module is connected to the main screw drive motor 17 to control the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18 via the main screw drive motor 17. In an embodiment with a screw propulsion motor 16, for example, the control module is connected to the screw propulsion motor 16 to control the screw propulsion motor 16 to drive the screw slag discharger in the settling and separation chamber 8 to rotate.

[0091] This design, on the one hand, allows the automated monitoring and control system to collect data on the liquid level, slurry density, and turbidity of the clarified liquid in the settling and separation chamber 8 in real time or at regular intervals. This data is then quickly analyzed and processed by the PLC control unit to accurately reflect the solid-liquid separation status and provide timely warnings of problems such as liquid level imbalance and abnormal particle settling. This avoids blockages or decreased separation efficiency caused by delayed manual monitoring, providing data support for stable system operation. On the other hand, the control module is linked with the main screw drive motor 17 and the screw propulsion motor 16. It can dynamically adjust the speed of the solid-liquid mixing propeller 5, the reaction stirring paddle 7, and the low-speed screw propeller 18 based on the monitoring data. It also adapts to the slag discharge rate of the screw slag discharger. For example, when the turbidity increases, the stirring speed is increased to enhance mixing, and when the liquid level is abnormal, the slag discharge rhythm is adjusted to maintain balance. This achieves a closed-loop control system of monitoring, analysis, and regulation, perfectly adapting to fluctuations in the solid-liquid ratio and different processing capacity requirements. On the other hand, automated control replaces manual operation, greatly reducing human intervention errors, lowering maintenance intensity and labor costs. At the same time, precise control ensures the stability of the 8-shaped flow field in the reaction chamber 6 and the efficient operation of the three-stage settling plate structure in the settling separation chamber 8, keeping the operating conditions of each stage of mixing, reaction, and separation in the optimal range.

[0092] To address the problems of low solid-liquid mixing efficiency, uneven reaction residence time, insufficient solid-liquid separation efficiency, reactor clogging, and weak automation control in traditional solid waste and carbon dioxide mineralization reaction technologies, some embodiments of the integrated absorption and mineralization technology utilize a mineralization reactor comprising a horizontal reactor body, a spiral propulsion system, and an automated monitoring and control system. Through a horizontal continuous flow design, a spiral composite mixing structure, and a multi-stage sedimentation separation structure, highly efficient coupling reaction and continuous solid-liquid separation can be achieved between pretreated industrial solid waste and recyclable carbon dioxide-rich liquid. For industrial solid waste including steel slag, carbide slag, fly ash, and mineral powder, and carbon dioxide-rich liquid including amine absorbent and carbonate absorbent, the technology achieves full solid-liquid coupling, controllable reaction residence time, efficient sedimentation, and continuous slag discharge. This enables integrated and efficient operation of carbon dioxide absorption, mineralization reaction, and regeneration separation, providing new equipment support for the industrialization of CCUS.

[0093] As an example, the horizontal reactor body is a sealed cylinder with an inner diameter of 0.8m to 2.0m and a length of 6m to 20m. The outer diameter of the screw propeller is 0.85 to 0.98 times the inner diameter of the cylinder, resulting in a length-to-diameter ratio (L / D) of 5 to 12, ensuring that the propulsion speed matches the processing capacity. This structure enables automated operation of the entire process of continuous feeding, mixing, sedimentation, and slag discharge of solid waste and carbon dioxide-rich liquid, ensuring that the material is fully mineralized within a reaction residence time of 1 to 2 hours and achieving continuous and stable operation. The solid-liquid mixing chamber 4 is equipped with a solid material propeller 3 to push solid waste into the reactor. Simultaneously, a solid-liquid mixing propeller 5 is provided, with regularly arranged circular holes and radial pins on its blades to ensure thorough dispersion of solid particles and uniform mixing with the slurry. The circular holes have a diameter of 10mm to 30mm and are arranged in a staggered pattern along the axial direction. The radial pins have a diameter of 8mm to 15mm, a length slightly smaller than the blade radius, and are arranged in rows of 4 to 8 pins with an axial spacing of 150mm to 300mm to improve the uniformity of solid-liquid mixing and reaction contact efficiency. The mineralization reactor used in the integrated absorption and mineralization technology is equipped with a level gauge, density meter, turbidity sensor, and PLC control unit to automatically adjust the solid-liquid ratio, reaction time, and slag discharge rate. The turbidity sensor signal, after PLC processing, can automatically adjust the rotation speed of the propeller system and the operating rhythm of the slag discharger to maintain the reaction system in an optimal solid-liquid equilibrium state. The solid-liquid mixing propeller 5, the coaxial forward and reverse spiral propulsion mixing structure, and the arrangement of each settling plate ensure uniform residence time distribution and controllable shear rate of the slurry, thereby improving the Ca2+ efficiency. 2+ / Mg 2+ The reaction efficiency with carbon dioxide and the carbonate yield; the overall reactor has the function of continuous mixing, reaction and separation, with a compact structure and stable operation, and is suitable for continuous industrial production of solid waste coupled with carbon dioxide-rich liquid mineralization.

[0094] The following examples illustrate this further with reference to actual production. In some embodiments, the mineralization reactor used in the integrated absorption and mineralization technology uses fly ash as the mineralization solid waste raw material. The main components of fly ash are: CaO 10% to 15%, MgO 3% to 5%, SiO2 40% to 50%, and Al2O3 20% to 25%. A carbon dioxide-rich solution formed after absorbing carbon dioxide from coal-fired flue gas using a 25wt% to 35wt% monoethanolamine (MEA) solution is used as the mineralization medium. Absorption and mineralization are carried out continuously under fixed operating conditions.

[0095] like Figure 1 and Figure 2As shown, the mineralization reactor used in the integrated absorption and mineralization technology is a horizontal sealed cylindrical structure. For example, it is made of alkali-resistant and corrosion-resistant 316L stainless steel or enamel-lined carbon steel. The two ends of the horizontal sealed cylindrical body are sealed to the inlet and outlet systems via flanges. The reactor is arranged horizontally in the following order: main screw drive motor 17, solid waste inlet 1, carbon dioxide rich liquid inlet 2, solid-liquid mixing chamber 4, reaction chamber 6, sedimentation separation chamber 8, regenerated liquid overflow port 13, solid-liquid separation viewing window 14, solid product outlet 15, and screw propulsion motor 16. The two ends of the cylinder are equipped with removable end caps for equipment maintenance and cleaning. The overall structure is compact and highly sealed, and it can operate stably under normal pressure or slightly positive pressure, such as 0 to 0.05 MPa.

[0096] As an example, the mineralization reactor used in the integrated absorption and mineralization technology includes a sealed cylinder, a spiral propulsion system, a heating and insulation system, a sedimentation and separation system, and an automated monitoring and control system. It can achieve fully automated operation of the continuous feeding, mixing, reaction, separation, and slag discharge of solid waste and carbon dioxide-rich liquid. The horizontal reactor body has the following structural dimensions: inner diameter of the cylinder 0.8m to 2.0m, length 6m to 20m, length-to-diameter ratio 5 to 12, corresponding to a processing capacity of 1t / h to 20t / h of solid material. The outer wall of the horizontal reactor body is covered with an insulation layer to prevent heat loss. Depending on the application scenario, circulating hot water, low-pressure steam, or waste heat from flue gas can be introduced into the jacket to maintain the reaction temperature at 30℃ to 60℃, and the heat medium temperature is controlled at 50℃ to 90℃.

[0097] As an example, the mineralization reactor used in the integrated absorption and mineralization technology has a total length of 10m to 14m, an inner diameter of 1.0m to 1.4m, and a shell material of 316L stainless steel. It is equipped with an external circulating hot water jacket, and the heat medium temperature is 55℃ to 65℃. The reaction temperature is maintained at 40℃ to 50℃, the operating pressure is atmospheric pressure, the solid-liquid ratio is 80g / L to 120g / L, and the fly ash particle size D... 50 The particle size is 50μm to 80μm, and the carbon dioxide loading in the carbon dioxide-rich solution is 0.30 to 0.40 mol carbon dioxide / mol MEA. Solid waste is continuously injected into the solid-liquid mixing chamber 4 via a screw feeder from the solid waste inlet 1 at a feed rate of 8 kg / min to 12 kg / min; carbon dioxide-rich solution is continuously injected into the solid-liquid mixing chamber 4 via a metering pump from the carbon dioxide-rich solution inlet 2 at a feed rate of 80 L / min to 120 L / min, corresponding to a slurry flow rate of approximately 0.1 m³ / min. 3 / min to 0.15m 3 / min.

[0098] As an example, solid waste is stably propelled along the conveying direction 19 (i.e., the axial direction of the cylinder) by the solid material propeller 3, and merges with the carbon dioxide-rich liquid in the solid-liquid mixing chamber 4. The solid-liquid mixing propeller 5 is driven by a variable frequency motor, and the blades have evenly spaced circular holes with a diameter of 10m to 30m arranged in an axially staggered pattern. Radial pins with a diameter of 8mm to 15mm are welded to the main shaft between the blades, with 4 to 8 pins per row and an axial spacing of 150mm to 300mm. Figure 3 and Figure 4 As shown. During operation, the disturbance from the circular jet and the shearing action of the pins together form a multi-directional turbulent flow field and a local high-shear zone, causing solid particles to break up and agglomerate rapidly, resulting in thorough solid-liquid mixing and uniform slurry concentration. The rotational speed in the mixing section is 20 rpm to 40 rpm, the liquid linear velocity is 0.05 m / s to 0.1 m / s, and the mixing uniformity coefficient is not less than 0.9.

[0099] As an example, the mixed slurry is spirally propelled into reaction chamber 6. This section is externally equipped with a jacketed heating device, through which circulating hot water or low-pressure steam at 40°C to 60°C is supplied, and a temperature sensor and automatic regulating valve are installed to maintain a constant temperature. Inside reaction chamber 6 is a reaction stirring paddle 7, with forward blades having a pitch of 300mm to 500mm and an inclination angle of 45° to 60° for material propulsion; and reverse blades having a pitch of 150mm to 250mm and an inclination angle of 60° to 75° for generating localized backflow. The two sets of blades are staggered, with an axial projection overlap of 30% to 50% and a blade area ratio of 1.5:1 to 2:1.

[0100] As an example, such as Figure 5 and Figure 6 As shown, the coaxial helical propulsion blades of the reaction impeller 7 create a continuous ∞-shaped circulating flow field in the axial section region of the reaction zone, causing local backflow and a high-shear zone to occur simultaneously during the axial propulsion of the slurry, resulting in a uniform residence time distribution of the reactants. The propulsion speed of the reaction chamber 6 is 5 rpm to 20 rpm, the axial propulsion velocity of the slurry is 0.02 m / s to 0.08 m / s, and the overall residence time of the reaction chamber 6 is controlled between 1 hour and 2 hours. The jacketed circulating hot water is controlled by a PID automatic regulating valve, ensuring that the reaction temperature fluctuation does not exceed ±3℃ and the system pH is maintained within the range of 8.0 to 9.5.

[0101] As an example, the reacted slurry transitions into the settling and separation chamber 8 via the flow guide buffer channel 9. A low-speed screw propeller 18 is installed within the flow guide buffer channel 9, rotating at 5 to 15 rpm. It employs large-pitch blades with a pitch of not less than 400 mm and an inclination angle of 60° to 75°. Four to eight inverted conical funnel outlets are evenly distributed along the propulsion direction, ensuring uniform distribution of the slurry along the width of the cylinder and preventing sedimentation and short-circuiting. The flow guide buffer channel 9 can also be called a buffer section; its design helps ensure a smooth transition of slurry flow velocity, thus facilitating particle settling.

[0102] As an example, the settling separation chamber 8 adopts a three-layer modular staggered settling plate structure, such as... Figure 4 As shown. The three layers of settling plates maintain a spacing of 50 to 80 mm, and are staggered so that the outflow area of ​​the upper plate faces the inflow area of ​​the lower plate, forming a natural graded buffer and flow transition zone. From top to bottom, the layers are: the first settling plate 10 (coarse separation layer), the second settling plate 11 (main settling layer), and the third settling plate 12 (fine separation layer). All three sets of settling plates are made of alkali-resistant stainless steel or high-polymer anti-corrosion materials. The plate surface is CNC molded, resulting in a smooth and flat surface with excellent anti-scaling and anti-clogging properties.

[0103] As an example, the first settling plate 10 has an inclination angle of 55° to 65° and a plate spacing of 40mm to 60mm. The plate surface is provided with triangular guide protrusions extending along the liquid flow direction, forming a 25° to 35° guiding angle with the flow direction to guide large particles to slide down quickly. The guide protrusions adopt a gradually increasing design, with the height gradually increasing from 5mm to 7mm to 7mm to 9mm along the flow direction, and the center-to-center spacing being 80mm to 100mm. In the initial stage of the liquid flow entering the settling section, it rapidly stratifies within the low-resistance guiding zone. Large particles slide down the plate surface under the action of gravity and guiding force. The increased height of the protrusions in the later stages forms a low-inlet, high-outlet guiding slope, further enhancing the particle sliding potential energy, allowing incompletely settled particles to quickly enter the bottom slag collection area.

[0104] As an example, the second settling plate 11 has an inclination angle of 50° to 60°, a plate spacing of 35mm to 45mm, and a continuous wave-shaped protrusion structure on its surface. The waveform geometry gradually changes along the flow direction: the wave height gradually increases from 3mm to 5mm to 5mm to 7mm, and the wavelength decreases from 60mm to 80mm to 50mm to 70mm. The gentle waveform at the inlet end can create flexible disturbances in the medium-speed liquid flow, preventing the upper flocs from being destroyed; the gradually increasing wave amplitude and denser wavelength along the flow path cause the liquid flow velocity to fluctuate periodically, generating multi-scale micro-vortices, thereby enhancing the collision and aggregation of medium-sized particles, forming larger particle clusters, and accelerating settling.

[0105] As an example, the third settling plate 12 has an inclination angle of 45° to 55°, a plate spacing of 25mm to 35mm, and an interlaced matrix of hemispherical protrusions on its surface. The protrusions have a diameter of 8mm to 10mm, and their height gradually increases from 3mm to 5mm to 5mm to 7mm. The center-to-center spacing decreases from 40mm to 60mm to 30mm to 50mm. This gradually increasing density arrangement on the plate surface creates a dense micro-disturbance zone and a deceleration zone effect, which significantly reduces the flow velocity and lengthens the flow path in the terminal region, allowing fine particles to remain sufficiently and complete sedimentation.

[0106] As an example, the slurry undergoes coarse separation, main settling, and fine separation processes sequentially within the settling chamber 8, with particles sliding down to the bottom slag collection area in stages. A spiral slag discharger is installed at the bottom of the settling chamber 8, driven by a spiral propulsion motor 16, such as a variable-speed motor, with a rotation speed of 3 to 10 rpm. The speed can be automatically adjusted according to the liquid level signal to achieve continuous discharge of solid products, which include calcium carbonate and other substances. During operation, the flow rate is controlled between 0.01 m / s and 0.02 m / s, resulting in distinct stratification of the slurry within the three-layer plate area: a clear, transparent upper layer, a slowly settling middle layer of particles, and a uniformly accumulated lower layer of solids.

[0107] As an example, the upper right part of the sedimentation separation chamber 8 is equipped with a regenerated liquid overflow port 13. The clarified supernatant is collected by the overflow weir and flows into the regenerated liquid return pipeline, and is sent back to the amine absorption tower for solvent reuse, realizing a closed-loop cycle. When the turbidity of the clarified liquid does not exceed 30 NTU to 50 NTU, the MEA concentration is maintained at 90% to 97% of the initial value, and the carbon dioxide load is about 0.04 mol / mol to 0.06 mol / mol, the regenerated liquid can be directly returned for reabsorption.

[0108] As an example, a solid-liquid separation viewing window 14 is provided on the side wall of the sedimentation separation chamber 8 for real-time monitoring of the sedimentation layer interface, liquid level, and particle distribution. A level gauge, density meter, and turbidity sensor are installed in corresponding positions. Data is collected and processed by the PLC system, which automatically adjusts the slag discharge rate and liquid inflow to ensure stable system operation. The bottom solid product is continuously discharged from the solid product outlet 15 via a spiral slag discharger at a speed of 4 to 6 rpm.

[0109] As an example, the mineralization reactor used in the integrated absorption and mineralization technology is equipped with level gauges, density meters, and turbidity sensors throughout the process, and the signals are acquired and processed by a PLC. The control system adjusts the speed of the screw propulsion motor 16 and the main screw drive motor 17 in real time, for example, from 5 rpm to 20 rpm, and the slag discharge frequency from 0.5 times / h to 5 times / h, to maintain a constant solid-liquid ratio, liquid level, and residence time. When the liquid level in the settling zone exceeds the set value, the slag discharge rate is automatically increased; when the slurry density decreases, the discharge rate is automatically reduced and the residence time is extended, achieving intelligent self-balancing control. The equipment has automatic slag discharge and liquid level alarm functions. During shutdown maintenance, manual cleaning can be performed through the bottom slag discharge port and inspection port, or online flushing can be performed through circulating cleaning fluid to prevent scaling and deposition.

[0110] This design, through the installation of a solid material propeller 3, a solid-liquid mixing propeller 5, and coaxial double-helix stirring blades within the horizontal cylinder, achieves continuous conveying and enhanced mixing of the slurry. This structure can create a dynamic flow field of "propulsion-recirculation-remixing" within the reaction zone, ensuring uniform axial and radial contact between the carbon dioxide-rich liquid and the calcium- and magnesium-containing solid waste, significantly improving the Ca... 2+ / Mg2+ The dissolution rate and carbon dioxide mineralization reaction rate are optimized to avoid the localized deposition and clogging problems common in high-solids systems. On the other hand, the guide buffer channel 9 employs a low-speed, large-pitch screw propeller and an inverted conical funnel slurry outlet structure, enabling a smooth transition and wide, uniform distribution of slurry flow velocity. This avoids short-circuiting, turbulence, and dead zones in the settling zone, providing stable inflow conditions for subsequent settling separation. Furthermore, a three-layer progressively higher functional raised settling plate structure is proposed. Through a graded design of a coarse separation layer, a main settling layer, and a fine separation layer, the settling flow field is gradually refined along the flow direction. The progressively higher guiding protrusions in the first layer guide large particles to slide down rapidly; the progressively higher and denser waveform protrusions in the second layer enhance the flocculation and settling of medium-sized particles; and the progressively higher lattice protrusions in the third layer extend the settling path of fine particles, achieving efficient end-stage collection. This structure enables the solid-liquid separation process to achieve a gradient evolution of sliding-slow settling-clarification, resulting in high separation efficiency and resistance to clogging. On the other hand, an adjustable-speed spiral slag discharger is installed at the bottom of the settling zone to achieve continuous and automatic discharge of mineralized products; a regeneration liquid overflow port 13 is installed at the top to recover clarified liquid. Combined with a level gauge, density meter, and PLC control system, intelligent control of reaction time, solid-liquid ratio, and slag discharge rate can be achieved, thereby maintaining stable operation of the system under optimal solid-liquid equilibrium. Furthermore, compared with traditional vertical spray towers, bubble towers, and other intermittent reaction devices, the reactor in this embodiment has significant advantages such as compact structure, controllable flow field, continuous operation, high separation efficiency, and excellent anti-clogging performance. It can operate stably in high-solid-content systems with high solid-liquid ratios, significantly improving carbon dioxide conversion rate and carbonate yield, providing efficient and reliable equipment support for the continuous and industrial application of integrated absorption and mineralization processes.

[0111] It should be noted that other embodiments of this application also include a mineralization reactor and mineralization reaction method for an integrated absorption and mineralization technology that can be implemented, formed by combining the technical features of the above embodiments.

[0112] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0113] The embodiments described above are merely illustrative of several implementation methods of this application, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the patent application. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this application, and these all fall within the scope of protection of this application. Therefore, the patent protection scope of this application should be determined by the appended claims.

Claims

1. A mineralization reactor for integrated absorption and mineralization technology, characterized in that, Includes the horizontal reactor body; The horizontal reactor body has a solid waste inlet (1) and a solid product outlet (15) at both ends, and between the solid waste inlet (1) and the solid product outlet (15), along the conveying direction (19), the interior of the horizontal reactor body is sequentially provided with a solid-liquid mixing chamber (4), a reaction chamber (6), a flow guide buffer channel (9) and a sedimentation separation chamber (8). The horizontal reactor body is also provided with a carbon dioxide rich liquid inlet (2) that connects to the solid-liquid mixing chamber (4), and a solid-liquid mixing propeller (5) is provided in the solid-liquid mixing chamber (4), a reaction stirring paddle (7) is provided in the reaction chamber (6), a low-speed spiral propeller (18) is provided in the flow guide buffer channel (9), and at least two layers of modular staggered settling plate structure are provided in the settling separation chamber (8). The reaction stirring paddle (7) is a coaxial spiral propulsion stirring structure.

2. The mineralization reactor for the integrated absorption and mineralization technology according to claim 1, characterized in that, The settling plate structure includes a first settling plate (10), a second settling plate (11) and a third settling plate (12), wherein the first settling plate (10) is located between the flow guide buffer channel (9) and the second settling plate (11), and the third settling plate (12) is located between the second settling plate (11) and the solid product outlet (15).

3. The mineralization reactor for the integrated absorption and mineralization technology according to claim 1, characterized in that, In the direction of gravity during use, the horizontal reactor body is provided with a spiral slag discharger at the bottom of the sedimentation separation chamber (8). The spiral slag discharger is used to continuously discharge mineralized solids through the solid product outlet (15) under the drive of the spiral propulsion motor (16).

4. The mineralization reactor for the integrated absorption and mineralization technology according to claim 3, characterized in that, The mineralization reactor used in the integrated absorption and mineralization technology also includes the spiral propulsion motor (16), the output end of which passes through the solid product outlet (15) and is connected to the spiral slag discharger.

5. The mineralization reactor for the integrated absorption and mineralization technology according to claim 1, characterized in that, The blades of the solid-liquid mixing propeller (5) are provided with regularly arranged circular holes and radial pins to achieve dispersion of solid particles and uniform mixing of slurry.

6. The mineralization reactor for the integrated absorption and mineralization technology according to claim 1, characterized in that, In the direction of gravity during use, the horizontal reactor body has a regenerated liquid overflow port (13) in the middle of the sedimentation separation chamber (8), and an overflow weir and / or filter body are provided at the regenerated liquid overflow port (13) for recycling liquid through the regenerated liquid overflow port (13); or, The horizontal reactor body is provided with a solid material screw propeller (3) in the solid-liquid mixing chamber (4), or a solid material screw propeller (3) is provided between the solid waste inlet (1) and the solid-liquid mixing chamber (4); or, The horizontal reactor body is provided with a solid-liquid separation viewing window (14) at the solid-liquid mixing chamber (4) or the sedimentation separation chamber (8); or, The horizontal reactor body is provided with a heating jacket outside the reaction chamber (6) or outside the horizontal reactor body; or, The horizontal reactor body is equipped with detachable end caps at both ends.

7. The mineralization reactor for the integrated absorption and mineralization technology according to claim 1, characterized in that, The solid-liquid mixing propeller (5), the reaction stirring paddle (7), and the low-speed screw propeller (18) are arranged coaxially.

8. The mineralization reactor for the integrated absorption and mineralization technology according to claim 7, characterized in that, The mineralization reactor used in the integrated absorption and mineralization technology also includes a main spiral drive motor (17), the output end of which passes through the solid waste inlet (1) and is integrated with the solid-liquid mixing propeller (5), the reaction stirring paddle (7) and the low-speed spiral propeller (18).

9. The mineralization reactor for the integrated absorption and mineralization technology according to any one of claims 1 to 8, characterized in that, The mineralization reactor used in the integrated absorption and mineralization technology also includes an automated monitoring and control system, which is equipped with a control module, a level gauge, a density meter, a turbidity sensor, and a PLC control unit. The level gauge, the density meter and the turbidity sensor are respectively disposed in the sedimentation separation chamber (8), and the PLC control unit is respectively connected to the level gauge, the density meter and the turbidity sensor; The control module is connected to the solid-liquid mixing propeller (5), the reaction stirring paddle (7), and the low-speed screw propeller (18), respectively.

10. A mineralization reaction method for integrated absorption and mineralization technology, characterized in that, The mineralization reactor used in the integrated absorption and mineralization technology according to any one of claims 1 to 9, wherein the mineralization reaction method of the integrated absorption and mineralization technology includes the following steps: The pretreated calcium-magnesium solid waste enters the solid-liquid mixing chamber (4) through the solid waste inlet (1); Carbon dioxide-rich liquid enters the solid-liquid mixing chamber (4) through the carbon dioxide-rich liquid inlet (2); Using the regularly arranged circular holes and radial pins on the blades of the solid-liquid mixing propeller (5), calcium-magnesium solid waste is mixed with carbon dioxide-rich liquid in the solid-liquid mixing chamber (4) to form a slurry, which is then sent into the reaction chamber (6). Within the preset temperature range, after the carbon dioxide mineralization reaction is carried out in the reaction chamber (6) using a coaxial spiral propulsion stirring structure, the slurry after the reaction is sent into the guide buffer channel (9). The reacted slurry is evenly distributed into the settling and separation chamber (8) through the flow guide buffer channel (9); The reacted slurry settles in the settling separation chamber (8) in stages, and the mineralized solid products in the bottom slag collection area (20) are discharged through the spiral slag discharger.

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