System and method for carbon dioxide capture and co-mineralization of solid waste to produce negative carbon products

Abstract

The application discloses a system and method for preparing negative carbon products by simultaneously mineralizing solid waste and capturing carbon dioxide, and relates to the technical field of CO2 capture, utilization and storage. The system comprises a pretreatment device, a carbon dioxide absorption device for absorbing and capturing carbon dioxide by using composite amine solution to generate rich amine solution, a solid waste leaching device for leaching solid waste materials to generate leaching residues and a post-leaching mixed solution, a mineralization reaction device for mineralization reaction of the post-leaching mixed solution to generate a post-mineralization mixed solution containing nano calcium carbonate and release regenerated amine solution by amine non-thermal regeneration, a double negative carbon product preparation device and a control unit. The application realizes the purposes of energy saving, high utilization rate, environmental protection and wide adaptability by system coupling innovation, material system optimization and process mechanism breakthrough, and constructs a closed-loop integrated system of "industrial flue gas CO2 capture-multiple source solid waste resourceization-double high-value product preparation".

Description

Technical Field

[0001] This invention relates to the field of CO2 capture, utilization and storage technology, and in particular to a system and method for the co-processing of carbon dioxide capture with solid waste mineralization to prepare negative carbon products. Background Technology

[0002] The urgency of CO2 capture and resource recovery in the context of global carbon neutrality. Since the Industrial Revolution, the combustion of fossil fuels has led to atmospheric CO2 concentrations exceeding 420 × 10⁻⁶. －6 This has led to frequent extreme weather events. Statistics from the International Energy Agency (IEA) show that global energy-related CO2 emissions reach 36.8 billion tons per year, with industrial processes (steel, cement, chemicals, etc.) accounting for over 35%. Against this backdrop, carbon capture, utilization, and storage (CCUS) is widely recognized as a core technological pathway to achieving carbon neutrality, with an estimated need to store over 7 billion tons of CO2 per year by 2050.

[0003] Bottlenecks in existing CO2 capture technology: (1) Although the current mainstream chemical absorption methods (such as monoethanolamine MEA, diethanolamine DEA, etc.) have high collection efficiency (>90%), they have two major problems: High regeneration energy consumption: Traditional amine methods require high-temperature (100-120℃) steam desorption, which accounts for 60%-70% of the total system cost. Moreover, high temperature accelerates amine degradation (e.g., MEA annual degradation rate >20%), leading to equipment corrosion and increased operating costs.

[0004] Insufficient utilization of solid waste resources: The annual output of industrial solid waste (steel slag, carbide slag, etc.) exceeds 4 billion tons, but existing treatment technologies (such as landfill and brick making) can only achieve low-value-added utilization, and its alkaline components (Ca) are not fully utilized. 2+ Mg 2+ It has not been effectively used for CO2 mineralization, resulting in resource waste and secondary pollution.

[0005] (2) Current status and challenges of CO2 mineralization technology: Mineralization technology involves the reaction of CO2 with alkaline minerals to generate stable carbonates (such as CaCO3 and BaCO3), but existing technologies have significant drawbacks: Raw material limitations: It relies on natural limestone (CaCO3) or single components of industrial solid waste (such as steel slag), failing to achieve the synergistic utilization of multi-source solid waste, and Ca... 2+ Low utilization rate (<50%).

[0006] Low added value of products: Micron-sized calcium carbonate (particle size > 1 μm) is generated, with a small specific surface area (< 10 m² / g), which makes it difficult to meet the needs of high-end materials (such as coatings and pharmaceutical fillers that require nano-sized products).

[0007] Poor process coupling: The mineralization and capture systems operate independently and require additional thermal energy to drive them, resulting in low overall energy efficiency.

[0008] In summary, existing technologies cannot simultaneously address the pain points of "high energy consumption and low mineralization efficiency in organic amine regeneration", "difficult cross-media utilization of alkaline solid waste", and "low added value of products". There is an urgent need to develop new integrated absorption-mineralization technologies to achieve the synergistic goals of reducing energy consumption, increasing the value of solid waste, and converting CO2 to high value.

[0009] There is an existing integrated CO2 absorption-mineralization process based on a mixed amine solution (publication number CN118987899A), which has the following problems: Lack of solid waste utilization and high costs: Using high-purity CaO at 800 yuan / ton accounts for 45% of the raw material cost, and the cost of treating 1 ton of CO2 is about 300 yuan, with no reduction in solid waste. The product has low added value and is not at the nanoscale. Poor amine solution circulation and short lifespan: Direct circulation of filtrate leads to impurity accumulation; after 50 cycles, the PZ degradation rate is 12%, the absorption capacity decreases from 0.52 to 0.38 mol / mol (a 27% decrease), and the operation and maintenance cost increases by 20%. Low integration and high energy consumption: There is no reactive heat recovery and no energy coupling, and the total energy consumption is 50% higher than the target of this invention.

[0010] There is another existing technology for preparing carbon-fixing proppant based on the mineralization reaction of coal thermal power solid waste and carbon dioxide, and its application (publication number CN118995190A). Its problems include: Single product: Unpurified calcium carbonate, missing out on high added value; The adsorbent is expensive: the degradation rate is 10% per batch, the replenishment amount is 4.2 kg / tCO2, accounting for 38% of the cost (320 yuan per ton of CO2). High voltage is uneconomical: 3-5MPa requires specialized equipment, increasing investment by 60%, and high voltage has a high proportion of energy consumption; Low utilization rate of solid waste: only 35-40% of the active components are dissolved, and more than 60% of the residue is landfilled.

[0011] Therefore, based on years of experience and practice in related industries, the inventor proposes a system and method for preparing negative carbon products through carbon dioxide capture and solid waste mineralization, in order to overcome the shortcomings of existing technologies. Summary of the Invention

[0012] The purpose of this invention is to provide a system and method for preparing negative carbon products by carbon dioxide capture and solid waste mineralization, overcoming the problems of high regeneration energy consumption, low solid waste utilization rate, limited product added value, and narrow applicability in the existing technology. This invention constructs a closed-loop integrated system of "industrial flue gas CO2 capture - multi-source solid waste resource utilization - preparation of dual high-value products" through system coupling innovation, material system optimization, and process mechanism breakthrough, achieving the goals of energy saving, high utilization rate, environmental protection, and wide applicability.

[0013] The objective of this invention is achieved by providing a system for the synergistic production of negative carbon products through carbon dioxide capture and solid waste mineralization, comprising: Pretreatment device for pre-treating flue gas; A carbon dioxide absorption device for absorbing and capturing carbon dioxide in a composite amine solution to generate a rich amine solution; the pretreatment device is connected to the bottom of the carbon dioxide absorption device; Solid waste leaching device used for leaching solid waste materials to generate leaching residue and leaching mixture; A mineralization reaction device is used to generate a mineralized mixture containing nano-calcium carbonate through a mineralization reaction of the leaching mixture, and to release regenerated amine liquid through non-thermal amine regeneration. The solid waste leaching device is connected to the mineralization reaction device through a leaching mixture output pipeline; the bottom of the carbon dioxide absorption device is connected to the mineralization reaction device through a rich amine liquid output pipeline; and the mineralization reaction device is connected to the top of the carbon dioxide absorption device through a regenerated amine liquid pipeline. A dual-negative carbon product preparation device includes a nano-calcium carbonate purification section for purifying the mineralized mixture to produce nano-calcium carbonate, and a cementitious material preparation section for hydrating the residue after reaction under the action of a cementitious activator to produce a cementitious material. The mineralization reaction device is connected to the nano-calcium carbonate purification section through a mineralized mixture output pipeline. The solid waste leaching device and the nano-calcium carbonate purification section are connected to the cementitious material preparation section through a residue pipeline. The control unit is electrically connected to the pretreatment device, the carbon dioxide absorption device, the solid waste leaching device, the mineralization reaction device, and the dual negative carbon product preparation device.

[0014] In a preferred embodiment of the present invention, the mineralization reaction device is connected to a carbon dioxide delivery pipeline for outputting carbon dioxide gas, the cementitious material preparation unit includes a hydration reaction heat exchange structure, and the carbon dioxide delivery pipeline is connected to the bottom of the carbon dioxide absorption device after heat exchange through the hydration reaction heat exchange structure.

[0015] In a preferred embodiment of the present invention, the nano-calcium carbonate purification unit is connected to the solid waste leaching device through a first filtrate conveying pipeline for conveying the remaining filtrate after purification of the mineralized mixture, and the cementitious material preparation unit is connected to the solid waste leaching device through a second filtrate conveying pipeline for conveying the remaining filtrate after the hydration reaction.

[0016] In a preferred embodiment of the present invention, the carbon dioxide absorption device includes a carbon dioxide absorption tower, and the pretreatment device is connected to the bottom of the carbon dioxide absorption tower through a pretreatment flue gas pipeline; the top of the carbon dioxide absorption tower is connected to a composite amine liquid input pipeline and a clean flue gas discharge pipeline, and an amine liquid buffer zone is provided at the bottom of the carbon dioxide absorption tower.

[0017] In a preferred embodiment of the present invention, the carbon dioxide absorption tower is a packed tower, the inner cavity of the packed tower is provided with stepped ring packing in layers, a liquid distributor is provided at the top of the inner cavity of the packed tower, the composite amine liquid input pipeline is connected to the liquid distributor, and the amine liquid buffer zone is provided at the bottom of the inner cavity of the packed tower; the pretreatment device is connected to the bottom of the packed tower, and the clean flue gas discharge pipeline is provided at the top of the packed tower.

[0018] In a preferred embodiment of the present invention, the composite amine liquid input pipeline is connected to an absorbent replenishment tank for supplying composite amine liquid to the carbon dioxide absorption tower. A metering pump is installed at the bottom of the absorbent replenishment tank, and a liquid level monitor is installed at the top of the absorbent replenishment tank.

[0019] In a preferred embodiment of the present invention, the solid waste leaching device includes an leaching container for leaching solid waste materials to generate leaching residue and leaching mixture, the leaching container being connected to a solid waste material input section and a co-extracting agent input section, the leaching container being connected to the mineralization reaction device through the leaching mixture output pipeline, and the leaching container being connected to the cementitious material preparation section through the residue pipeline.

[0020] In a preferred embodiment of the present invention, the extraction container is an extraction tank, an anchor-type stirrer is installed inside the extraction tank and attached to the tank wall, the top of the extraction tank is connected to the solid waste input section and the co-extracting agent input section, one side of the extraction tank is connected to the extraction mixture output pipeline, and a first one-way valve is installed on the extraction mixture output pipeline.

[0021] In a preferred embodiment of the present invention, the solid waste input section is a multi-source solid waste addition tank, the inner cavity of the multi-source solid waste addition tank is provided with a magnetic separation and impurity removal device, the bottom of the multi-source solid waste addition tank is provided with a variable frequency screw conveyor, and the outlet of the variable frequency screw conveyor is connected to the top of the extraction tank.

[0022] In a preferred embodiment of the present invention, the mineralization reaction apparatus includes a mineralization reaction container for generating a mineralized post-mineralized mixture containing nano-calcium carbonate through a mineralization reaction of the leaching post-mixture and for releasing regenerated amine liquid through non-thermal amine regeneration. The mineralization reaction container is connected to a mineralization regulator input section, and the leaching container is connected to the mineralization reaction container through the leaching post-mixture output pipeline. The carbon dioxide absorption tower is connected to the mineralization reaction container through a rich amine liquid output pipeline, and the mineralization reaction container is connected to the top of the carbon dioxide absorption tower through a regenerated amine liquid pipeline that allows the regenerated amine liquid to flow unidirectionally into the carbon dioxide absorption tower. A first circulation pump is installed on the rich amine liquid output pipeline, and a second circulation pump is installed on the regenerated amine liquid pipeline. The mineralization reaction container is connected to the bottom of the carbon dioxide absorption tower through the carbon dioxide delivery pipeline.

[0023] In a preferred embodiment of the present invention, the mineralization reaction container is a mineralization reactor, and a propeller-type agitator is installed inside the mineralization reactor. The top of the mineralization reactor is connected to the mineralization regulator input section, the extraction mixture output pipeline, and the amine-rich liquid output pipeline. The top of the mineralization reactor is also connected to the carbon dioxide delivery pipeline, and a second one-way valve is installed on the carbon dioxide delivery pipeline. A mineralization jacket for heating the mineralization reactor is installed on the side wall of the mineralization reactor, and a temperature control interface is installed on the mineralization jacket. An online particle size monitoring port is installed on the side wall of the mineralization reactor.

[0024] In a preferred embodiment of the present invention, the nano-calcium carbonate purification unit includes a first solid-liquid separation structure. The mineralization reaction containment unit is connected to the first solid-liquid separation structure through the mineralized mixture output pipeline. The first solid-liquid separation structure includes, in sequence, a ceramic membrane filter for retaining coarse residue in the mineralized mixture and for preliminarily purifying the nano-calcium carbonate suspension, a disc centrifuge for centrifugally separating the nano-calcium carbonate wet material and the mother liquor, a countercurrent washing tower for washing the nano-calcium carbonate wet material with purified water, and a first drying structure for drying the nano-calcium carbonate wet material. The ceramic membrane filter is connected to the cementitious material preparation unit through a residue pipeline, the disc centrifuge is connected to the extraction containment unit through the first filtrate delivery pipeline, and the first drying structure is provided with a nano-calcium carbonate finished product outlet.

[0025] In a preferred embodiment of the present invention, the gelling material preparation unit includes a hydration reaction container, the hydration reaction container is connected to a gelling activator input unit, the extraction container and the first solid-liquid separation structure are connected to the hydration reaction container through a residue pipeline, and the hydration reaction heat exchange structure is provided on the hydration reaction container. The hydration reaction containment is connected to the second solid-liquid separation structure, which includes a high-pressure plate and frame filter press for separating the gelled wet material and free water in the hydration reaction products, and a second drying structure for drying the gelled wet material, which are connected in sequence. The high-pressure plate and frame filter press is connected to the extraction containment through the second filtrate conveying pipeline, and the second drying structure is provided with a finished gelled material outlet.

[0026] In a preferred embodiment of the present invention, the hydration reaction containment is a pressurized reactor, the top of the pressurized reactor is connected to the gelling activator input section and the residue pipeline, and the inner cavity of the pressurized reactor is equipped with a paddle stirrer; the hydration reaction heat exchange structure is a hydration jacket disposed on the side wall of the pressurized reactor, and the hydration jacket is connected to the carbon dioxide delivery pipeline; the bottom of the pressurized reactor is connected to the second solid-liquid separation structure.

[0027] In a preferred embodiment of the present invention, the pretreatment device includes a cyclone separator, a bag filter and an alkaline spray tower. The bottom of the pretreatment device is provided with a flue gas inlet and the top of the pretreatment device is provided with a pretreated flue gas outlet. The pretreated flue gas outlet is connected to the bottom of the carbon dioxide absorption device through a pretreated flue gas pipeline.

[0028] The objective of this invention can also be achieved by providing a method for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization, implemented using the aforementioned system for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization; the method for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization includes: The flue gas enters the pretreatment unit for pretreatment; The pretreated flue gas is fed into a carbon dioxide absorption device, where a composite amine solution captures and absorbs the carbon dioxide in the pretreated flue gas, forming a rich amine solution. The solid waste leaching device connects the solid waste material input section and the co-extracting agent input section. The co-extracting agent leaches the solid waste material, dissolving the alkaline components in the solid waste material. The alkaline components are carried by the leached mixture to the mineralization reaction device. The leaching residue is output to the cementitious material preparation section. The leaching mixture containing alkaline components from the solid waste material in the solid waste leaching unit is output to the mineralization reaction unit. The carbon dioxide absorption unit supplies amine-rich solution to the solid waste leaching unit. Under the action of the mineralization regulator, the amine-rich solution reacts with the leaching mixture to generate a mineralized mixture containing nano-calcium carbonate. The regenerated amine solution and carbon dioxide gas are released through non-thermal amine regeneration. The carbon dioxide gas exchanges heat with the cementitious material preparation unit and then returns to the carbon dioxide absorption unit; the regenerated amine solution returns to the carbon dioxide absorption unit. After mineralization, the mixed liquid is output to the nano-calcium carbonate purification unit to be purified into nano-calcium carbonate product. The remaining filtrate after purification is returned to the solid waste leaching unit, and the residue intercepted after purification is output to the cementitious material preparation unit. The leaching residue and the purified intercepted residue undergo a hydration reaction in the cementitious material preparation section to generate the finished cementitious material. The remaining filtrate after hydration is returned to the solid waste leaching unit.

[0029] Based on the above, the system and method for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization of the present invention have the following beneficial effects: This invention achieves energy conservation through "integrated closed-loop + amine non-thermal regeneration," reducing system energy consumption by more than 30% compared to existing technologies. The invention achieves 100% landfill-free utilization of solid waste and ensures that flue gas pollutants meet emission standards, realizing "solid waste reduction + carbon sequestration" and achieving environmental protection goals. The invention's dual high-value products enhance system profitability, reducing processing costs by more than 25% compared to existing technologies, thus reducing economic costs. This invention is adaptable to various types of solid waste and flue gas, can be promoted without large-scale modifications, has a wide range of applications, and achieves universality. Attached Figure Description

[0030] The following figures are intended only to illustrate and explain the present invention and do not limit the scope of the invention. Wherein: Figure 1 This is a schematic diagram of the system for preparing negative carbon products by carbon dioxide capture and synergistic solid waste mineralization according to the present invention.

[0031] In the picture: 1. Pretreatment device; 101. Pretreatment flue gas pipeline; 2. Carbon dioxide absorption device; 201. Amine-rich liquid output pipeline; 2011. First circulation pump; 202. Compound amine liquid input pipeline; 203. Clean flue gas discharge pipeline; 21. Carbon dioxide absorption tower; 22. Absorbent liquid replenishment tank; 3. Solid waste leaching device; 301. Leached mixed liquor output pipeline; 3011. First check valve; 31. Leaching container; 32. Solid waste input section; 33. Co-extractant input section; 4. Mineralization reaction apparatus; 401. Carbon dioxide delivery pipeline; 4011. Second check valve; 402. Mineralized mixed liquid output pipeline; 403. Regenerated amine liquid pipeline; 4031. Second circulation pump; 41. Mineralization reaction container; 42. Mineralization regulator input section; 5. First solid-liquid separation structure; 501. First filtrate conveying pipeline; 502. Nano-calcium carbonate finished product outlet; 6. Hydration reaction container; 61. Hydration jacket; 62. Gelation activator inlet; 7. Second solid-liquid separation structure; 701. Second filtrate conveying pipeline; 702. Finished cementitious material outlet; 8. Residue pipeline. Detailed Implementation

[0032] To provide a clearer understanding of the technical features, objectives, and effects of the present invention, specific embodiments of the present invention will now be described with reference to the accompanying drawings.

[0033] The specific embodiments of the present invention described herein are for illustrative purposes only and should not be construed as limiting the invention in any way. Under the teachings of this invention, those skilled in the art can conceive of any possible modifications based on the invention, all of which should be considered within the scope of the invention. It should be noted that when an element is referred to as being "set on" another element, it can be directly on the other element or there may be an intervening element. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or there may be an intervening element. The terms "mounted," "connected," and "linked" should be interpreted broadly; for example, they can refer to mechanical or electrical connections, or internal communication between two elements, and can be direct or indirect connections through an intermediate medium. Those skilled in the art can understand the specific meaning of the above terms according to the specific circumstances. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and similar expressions used herein are for illustrative purposes only and do not represent the only possible embodiments.

[0034] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein in the specification of 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 herein includes any and all combinations of one or more of the associated listed items.

[0035] like Figure 1 As shown, this invention provides a system for the synergistic preparation of carbon-negative products through carbon dioxide capture and solid waste mineralization, comprising a pretreatment device 1, a carbon dioxide absorption device 2, a solid waste leaching device 3, a mineralization reaction device 4, a dual carbon-negative product preparation device, and a control unit; wherein: Pretreatment unit 1 is used to pretreat flue gas to adapt it to subsequent absorption requirements. Different specific configurations of pretreatment unit 1 can be adopted for different flue gas concentrations, as long as the CO2 concentration is 8%-40% and compatible with the pretreatment process. Through flue gas pretreatment, the system can adapt to low-concentration flue gas, without CO2 concentration, directly treating low-concentration industrial flue gas (CO2 volume fraction 8%-40%), reducing system investment by 25%-30% compared to technical solutions requiring CO2 concentration.

[0036] The carbon dioxide absorption device 2 is used to absorb and capture carbon dioxide in the composite amine liquid to generate a rich amine liquid; the pretreatment device 1 is connected to the bottom of the carbon dioxide absorption device 2; the amine liquid here is a composite amine absorbent, which includes a main absorbing amine and a catalytic amine. The main absorbing amine reacts chemically with CO2 in the flue gas to generate a rich amine liquid (containing carbamates). The catalytic amine increases the reaction rate through proton transfer and inhibits the degradation of the main absorbing amine.

[0037] Solid waste leaching device 3 is used to leach solid waste materials to generate leaching residue and post-leaching mixture. A synergistic leaching reaction occurs in solid waste leaching device 3, specifically including the dissolution of Ca from the solid waste by the acidic component (existing technology) in the leaching agent. 2+ / Mg 2+ Ca 2 + / Mg 2+ The extracted mixture is carried to the next process. A mineralization reaction device 4 is used to generate a mineralized mixture containing nano-calcium carbonate from the leaching mixture and to release regenerated amine liquid through non-thermal amine regeneration. The solid waste leaching device 3 is connected to the mineralization reaction device 4 via a leaching mixture output pipeline 301. The bottom of the carbon dioxide absorption device 2 is connected to the mineralization reaction device 4 via an amine-rich liquid output pipeline 201. The mineralization reaction device 4 is connected to the top of the carbon dioxide absorption device 2 via a regenerated amine liquid pipeline 403. The reaction takes place in the mineralization reaction device 4, including: Ca carried by the leaching mixture... 2+ / Mg 2+ CO3 in amine-rich liquid 2- The reaction produces nano-calcium carbonate (suspended in the mixed solution); the carbamates in the amine-rich solution decompose, releasing regenerated amine solution and CO2 gas, achieving non-thermal amine regeneration (based on the alkalinity of the mixed solution after extraction), without the need for high temperature and high pressure.

[0038] The dual-negative carbon product preparation device produces dual-negative carbon products with a carbon fixation rate ≥20% and economic value, specifically including nano-calcium carbonate products and (solid waste) cementitious materials. It includes a nano-calcium carbonate purification section and a cementitious material preparation section. The nano-calcium carbonate purification section is used to purify the mineralized mixture to generate the nano-calcium carbonate product. The cementitious material preparation section is used to hydrate the leaching residue under the action of a cementitious activator to generate the cementitious material product. The mineralization reaction device 4 is connected to the nano-calcium carbonate purification section through the mineralized mixture output pipeline 402. The solid waste leaching device 3 and the nano-calcium carbonate purification section are connected to the cementitious material preparation section through the residue pipeline 8.

[0039] The control unit is electrically connected to the pretreatment unit 1, the carbon dioxide absorption unit 2, the solid waste leaching unit 3, the mineralization reaction unit 4, and the dual negative carbon product preparation unit. The control unit is used for system monitoring and regulation to ensure stable system operation.

[0040] This invention constructs a closed-loop integrated system of "industrial flue gas CO2 capture - multi-source solid waste resource utilization - dual high-value product preparation" through system coupling innovation, material system optimization and process mechanism breakthrough, which solves the defects of existing technologies such as high energy consumption, low solid waste utilization rate and single product.

[0041] This invention adopts an integrated closed-loop system: through the system coupling of "pretreatment-absorption-extraction-mineralization-dual product preparation", it can realize the internal circulation of materials (amine liquid, filtrate, etc.) and energy (waste heat), overcoming the defects of traditional process separation; This invention employs an "extraction-mineralization" coupling to reduce the energy consumption of organic amine regeneration: abandoning traditional thermal desorption or high-pressure reaction, it achieves non-thermal amine regeneration, reduces regeneration energy consumption, and simultaneously solves the two major pain points of "high energy consumption of amine regeneration and difficulty in solid waste utilization". This invention employs a dual-product synergistic preparation method: simultaneously preparing nano-calcium carbonate finished product and cementitious material finished product, thereby enhancing the system's economic value and carbon emission reduction benefits; This invention improves the overall utilization efficiency of solid waste. For various types of alkaline solid waste such as steel slag, fly ash, and coal-fired power plant solid waste, it achieves an active component leaching rate of ≥92% and converts 100% of solid waste residue into cementitious materials, eliminating the need for landfill disposal. This invention is suitable for low-concentration flue gas: it can directly treat industrial low-concentration flue gas (CO2 volume fraction 8%-40%) without CO2 concentration, and the system investment is reduced by 25%-30% compared with technical solutions that require concentration; This invention is applicable to various types of solid waste and flue gas from various industries, and is not limited to a specific type of solid waste or flue gas.

[0042] This invention achieves an environmentally friendly closed-loop system: leaching waste liquid and reaction tail gas are fully recovered, with no Cl. - Emissions of amines.

[0043] In summary, this invention achieves energy conservation through "integrated closed-loop + amine non-thermal regeneration," reducing system energy consumption by more than 30% compared to existing technologies. This invention achieves 100% utilization of solid waste (no landfill), and ensures that flue gas pollutants meet emission standards, realizing "solid waste reduction + carbon sequestration" and achieving environmental protection goals. The invention's dual high-value products enhance system profitability, reducing treatment costs by more than 25% compared to existing technologies, thus reducing economic costs. This invention is adaptable to various types of solid waste and flue gas, can be promoted without large-scale modifications, has a wide range of applications, and achieves universality.

[0044] Furthermore, such as Figure 1 As shown, the mineralization reaction device 4 is connected to a carbon dioxide delivery pipeline 401 for outputting carbon dioxide gas. The cementitious material preparation unit includes a hydration reaction heat exchange structure. After heat exchange through the hydration reaction heat exchange structure, the carbon dioxide delivery pipeline 401 is connected to the bottom of the carbon dioxide absorption device 2, so as to realize the effective recovery and utilization of the system's waste heat.

[0045] Furthermore, such as Figure 1 As shown, the nano-calcium carbonate purification unit is connected to the solid waste leaching device 3 through a first filtrate conveying pipeline 501 for conveying the remaining filtrate after purification of the mineralized mixture, and the cementitious material preparation unit is connected to the solid waste leaching device 3 through a second filtrate conveying pipeline 701 for conveying the remaining filtrate after the hydration reaction, thereby realizing the recycling of the system filtrate.

[0046] Furthermore, such as Figure 1 As shown, the carbon dioxide absorption device 2 includes a carbon dioxide absorption tower 21. The pretreatment device 1 is connected to the bottom of the carbon dioxide absorption tower 21 through the pretreatment flue gas pipeline 101. The top of the carbon dioxide absorption tower 21 is connected to the composite amine liquid input pipeline 202 and the clean flue gas discharge pipeline 203. An amine liquid buffer zone is set at the bottom of the carbon dioxide absorption tower 21.

[0047] The carbon dioxide absorption tower 21 can adopt various structural forms, including but not limited to packed towers, spray towers, membrane absorbers, etc., as long as it meets the requirements of "high-efficiency absorption + easy circulation".

[0048] Furthermore, such as Figure 1 As shown, the carbon dioxide absorption tower 21 is a packed tower (specifically, a vertical packed tower). The inner cavity of the packed tower is layered with stepped ring packing. A liquid distributor is installed at the top of the inner cavity of the packed tower. The composite amine liquid inlet pipe 202 is connected to the liquid distributor. An amine liquid buffer zone is installed at the bottom of the inner cavity of the packed tower. The pretreatment device 1 is connected to the bottom of the packed tower. A clean flue gas outlet pipe 203 is installed at the top of the packed tower.

[0049] Furthermore, such as Figure 1 As shown, the composite amine liquid inlet pipeline 202 is connected to the absorbent replenishment tank 22 for conveying composite amine liquid into the carbon dioxide absorption tower 21. A metering pump is installed at the bottom of the absorbent replenishment tank 22, and a liquid level monitor is installed at the top of the absorbent replenishment tank 22.

[0050] The composite amine liquid (composite amine absorbent) is evenly sprayed through the liquid distributor at the top of the packed tower and comes into countercurrent contact with the pretreated flue gas entering from the bottom of the packed tower. In the composite amine liquid, the main absorbing amine reacts with CO2 to generate a rich amine liquid, which catalyzes the amine to increase the reaction rate and inhibits degradation. The unabsorbed flue gas is discharged from the clean flue gas discharge pipeline 203 at the top of the tower and meets the emission standards. The rich amine liquid is discharged from the amine liquid buffer zone at the bottom of the packed tower.

[0051] The absorbent replenishment tank 22 is a vertical storage tank, located at the top auxiliary position of the system, and is connected to the top of the carbon dioxide absorption tower 21 through a metering pump and a compound amine liquid inlet pipeline 202.

[0052] The absorbent replenishment tank 22 stores fresh compound amine absorbent, and the liquid level monitor monitors the storage level in the tank in real time. When the amine concentration in the carbon dioxide absorption tower 21 is lower than the threshold for the appropriate absorption efficiency, the metering pump automatically replenishes fresh amine to ensure stable absorption efficiency.

[0053] Furthermore, such as Figure 1 As shown, the solid waste leaching device 3 includes an leaching container 31 for leaching solid waste materials to generate leaching residue and a post-leaching mixture. The leaching container 31 is connected to a solid waste material input section 32 and a co-extracting agent input section 33. The leaching container 31 is connected to a mineralization reaction device 4 via a post-leaching mixture output pipe 301, and to a cementitious material preparation section via a residue pipe 8. The co-extracting agent leaches the solid waste material, dissolving the alkaline components (Ca) in the solid waste material. 2+ / Mg 2 + After the alkaline components are extracted, the mixture is carried to the subsequent mineralization reaction device 4 for further reaction.

[0054] Furthermore, such as Figure 1 As shown, the leaching container 31 is an leaching tank (specifically, a horizontal stirred tank). An anchor-type agitator is installed inside the leaching tank, flush against the tank wall. The agitator shaft is connected to an external drive motor. The anchor-type agitator has the advantages of low speed and anti-deposition, making it suitable for high solids content systems within the leaching tank and preventing solid waste from settling at the bottom of the tank. The leaching tank can be a stirred tank or a tubular reactor / fluidized bed, as long as it meets the requirements of "leaching-mineralization synergy".

[0055] The top of the extraction tank is connected to the solid waste input section 32 and the co-extraction agent input section 33.

[0056] One side of the extraction tank is connected to the extraction mixture output pipeline 301. A first one-way valve 3011 is installed on the extraction mixture output pipeline 301, and a check valve core is installed inside the first one-way valve 3011 to adapt to the system pressure range. The first one-way valve 3011 prevents the high-pressure mineralizing liquid in the mineralization reaction device 4 (mineralization reaction vessel) from flowing back into the extraction tank, ensuring that the extraction-mineralization process proceeds in sequence.

[0057] Furthermore, the solid waste input section 32 is a multi-source solid waste addition tank. The inner cavity of the multi-source solid waste addition tank is equipped with a magnetic separation and impurity removal device. A variable frequency screw conveyor is installed at the bottom of the multi-source solid waste addition tank, and the outlet of the variable frequency screw conveyor is connected to the top of the extraction tank.

[0058] The multi-source solid waste addition tank is located at the top auxiliary position of the system. It adopts a double hopper structure to accommodate different types of solid waste. The two hoppers store different solid wastes such as steel slag and fly ash respectively, which can meet the needs of multiple scenarios. The magnetic separation and impurity removal device removes metal impurities from the solid waste to avoid damage to subsequent equipment. The variable frequency screw conveyor adjusts the solid waste feeding rate to meet the solid-liquid ratio requirements in the leaching tank.

[0059] Specifically, the top of the extraction tank is equipped with a solid waste inlet and an extractant inlet, and the outlet of the variable frequency screw conveyor is connected to the solid waste inlet; the co-extractant input unit 33 is connected to the extractant inlet.

[0060] The extraction tank is equipped with an extraction jacket on its side wall, and the extraction jacket has heating and cooling interfaces. The temperature is controlled to a suitable extraction temperature range through the extraction jacket.

[0061] Solid waste materials are fed into the solid waste inlet and mixed with the co-extraction agent; the anchor agitator promotes solid-liquid contact within the tank.

[0062] The synergistic extractant can be an organic acid system, or an inorganic acid system / complex acid system, to meet the requirement of "dissolving Ca". 2+ Simply add "suppress impurities".

[0063] Solid waste materials can be steel slag / fly ash, or red mud / phosphogypsum / carbide slag, containing alkaline components and suitable for leaching processes. A synergistic leaching agent is used to leach the solid waste materials, dissolving the alkaline components (Ca) from them. 2+ / Mg 2+ After the alkaline components are extracted, the mixture is carried to the subsequent mineralization reaction device 4 for further reaction.

[0064] Furthermore, such as Figure 1 As shown, the mineralization reaction device 4 includes a mineralization reaction container 41 for generating a mineralized mixture containing nano-calcium carbonate through a mineralization reaction of the leaching mixture and for releasing regenerated amine liquid through non-thermal amine regeneration. The mineralization reaction container 41 is connected to the mineralization regulator input unit 42. The leaching container 31 is connected to the mineralization reaction container 41 through the leaching mixture output pipeline 301. The mineralization reaction container 41 is connected to the bottom of the carbon dioxide absorption tower 21 through the carbon dioxide delivery pipeline 401.

[0065] The amine buffer zone of the carbon dioxide absorber 21 is connected to the mineralization reaction container 41 via the rich amine output pipeline 201. A first circulation pump 2011 is installed on the rich amine output pipeline 201, which transports the rich amine from the carbon dioxide absorber 21 to the mineralization reaction container 41 for non-thermal amine regeneration. The mineralization reaction container 41 is connected to the top of the carbon dioxide absorber 21 via the regenerated amine pipeline 403, which allows the regenerated amine to flow unidirectionally into the carbon dioxide absorber 21.

[0066] Ca in solid waste carried in the leachate mixture after extraction 2+ / Mg 2+ CO3 in amine-rich solution 2— The reaction produces calcium carbonate, and simultaneously releases regenerated amine liquid, achieving non-thermal amine regeneration. The mineralization regulator input section 42 contains a crystal growth inhibitor (existing technology) that limits the calcium carbonate particle size to the nanoscale, and a dispersant (existing technology) that prevents agglomeration.

[0067] The amine regeneration method in amine-rich solutions can be used for the regeneration of alkaline components in solid waste leachates, as well as for other low-energy regeneration methods, such as biological regeneration and membrane regeneration, without the need for high temperature / high pressure.

[0068] The outlet side of the mineralization reaction container 41 is connected to the regenerated amine liquid pipeline 403, and a second circulation pump 4031 is installed on the regenerated amine liquid pipeline 403. The second circulation pump 4031 transports the regenerated amine liquid in the mineralization reaction container 41 back to the top of the carbon dioxide absorption tower 21, forming a closed-loop circulation of the amine liquid. Specifically, the second circulation pump 4031 is a corrosion-resistant variable frequency centrifugal pump with a filter at the inlet (to prevent solid slag blockage) and a pressure regulating valve at the outlet. The variable frequency adjusts the flow rate to adapt to fluctuations in the CO2 concentration of the flue gas.

[0069] The outlet of the mineralization reaction container 41 is also connected to the nano-calcium carbonate purification unit, and the mineralized mixture flows to the nano-calcium carbonate purification unit for subsequent processes.

[0070] Furthermore, the mineralization reaction container 41 is a mineralization reactor, and a propeller-type agitator is installed inside the mineralization reactor. The agitator's stirring shaft is connected to an external drive motor. The propeller-type agitator has the advantages of high speed and strong dispersion, which is suitable for the growth requirements of nanocrystals inside the mineralization reactor and ensures the uniform action of the regulator.

[0071] like Figure 1 As shown, the top of the mineralization reactor is connected to the mineralization regulator input section 42 and the leaching mixture output pipeline 301 and the amine-rich liquid output pipeline 201. The top of the mineralization reactor is also connected to the carbon dioxide delivery pipeline 401. A second one-way valve 4011 (which can be called a carbon dioxide reflux valve) is installed on the carbon dioxide delivery pipeline 401. The second one-way valve 4011 contains a check valve core and is adapted to the system pressure range. The second one-way valve 4011 controls the unreacted CO2 generated by the mineralization reaction to flow back to the carbon dioxide absorption tower 21 for secondary collection, thereby improving carbon utilization.

[0072] The side wall of the mineralization reactor is equipped with a mineralization jacket for heating the reactor, and the mineralization jacket is equipped with a temperature control interface; the side wall of the mineralization reactor is equipped with an online particle size monitoring port.

[0073] The alkaline components (Ca) in the solid waste discharged from the extraction container 31 (extraction tank) 2+ / Mg 2+The leaching mixture of calcium carbonate and the amine-rich liquid from carbon dioxide absorption tower 21 are fed into the mineralization reactor, and a mineralization regulator is added. A propeller-type agitator is used to stir the mixture at high speed to promote crystal dispersion, and the temperature of the mineralization jacket is controlled to a suitable temperature range for mineralization. The crystal growth inhibitor (existing technology) in the mineralization regulator limits the calcium carbonate particle size to the nanoscale, and the dispersant (existing technology) prevents agglomeration.

[0074] Furthermore, such as Figure 1 As shown, the nano-calcium carbonate purification unit includes a first solid-liquid separation structure 5. The mineralization reaction container 41 is connected to the first solid-liquid separation structure 5 through a mineralized mixed liquid output pipeline 402. In a specific embodiment, the first solid-liquid separation structure 5 is a three-stage integrated structure. The first solid-liquid separation structure includes a ceramic membrane filter for intercepting coarse residue in the mineralized mixed liquid and for preliminary purification of the nano-calcium carbonate suspension, a disc centrifuge for centrifugal separation of nano-calcium carbonate wet material and mother liquor, a countercurrent washing tower for washing the nano-calcium carbonate wet material with purified water, and a first drying structure (such as a vacuum dryer) for drying the nano-calcium carbonate wet material. The ceramic membrane filter is connected to the cementitious material preparation unit through a residue pipeline 8. The disc centrifuge is connected to the extraction container 31 through a first filtrate conveying pipeline 501. The first drying structure is provided with a nano-calcium carbonate finished product outlet 502.

[0075] Specifically, a ceramic membrane filter traps coarse residues (a small amount of leaching residue mixed in the leaching solution) in the mineralization solution, and preliminarily purifies the nano-calcium carbonate suspension; a disc centrifuge separates the nano-calcium carbonate wet material from the mother liquor by centrifugal force; a countercurrent washing tower washes the wet material with purified water to remove residual regulators, and the filtrate after washing is returned to the leaching tank for reuse.

[0076] In addition to centrifugal separation, the first solid-liquid separation structure can also adopt a filtration + drying / membrane separation structure, as long as the "product purity / strength meets the standards".

[0077] Furthermore, such as Figure 1 As shown, the gelling material preparation unit includes a hydration reaction container 6, which is connected to a gelling activator input unit 62. The extraction container 31 and the first solid-liquid separation structure are connected to the hydration reaction container 6 through a residue pipeline 8. A hydration reaction heat exchange structure is provided on the hydration reaction container 6.

[0078] The hydration reaction containment 6 is connected to the second solid-liquid separation structure 7. The second solid-liquid separation structure 7 includes a high-pressure plate and frame filter press for separating the gelled wet material and free water in the hydration reaction products, and a second drying structure for drying the gelled wet material, which are connected in sequence. The high-pressure plate and frame filter press is connected to the extraction containment 31 through the second filtrate conveying pipeline 701. The second drying structure is provided with a gelled material finished product outlet 702.

[0079] Furthermore, such as Figure 1As shown, the hydration reaction container 6 is a pressurized reactor. The top of the pressurized reactor is connected to the gelling activator input section 62 and the residue pipeline 8. The pressurized reactor is a horizontal reactor, and a paddle agitator is installed in the inner cavity of the pressurized reactor. The hydration reaction heat exchange structure is a hydration jacket 61 installed on the side wall of the pressurized reactor. The hydration jacket 61 is connected to the carbon dioxide delivery pipeline 401. The bottom of the pressurized reactor is connected to the second solid-liquid separation structure 7.

[0080] The undissolved residue discharged from the leaching tank (leaching residue and coarse residue in the mineralization solution) is fed into a pressurized reactor, and a gelling activator is added. The waste heat from the tail gas of the mineralization reactor (i.e., heat exchange between the gas in the carbon dioxide delivery pipeline 401 and the hydration jacket 61) is used to heat the residue to a temperature range suitable for gelation. The alkaline component (existing technology) in the gelling activator activates the active SiO2 / Al2O3 within the residue, generating hydrated calcium silicate (gelling core). The setting time is controlled by the setting agent (existing technology). The waste heat reused in the pressurized reactor can be the aforementioned waste heat from the tail gas of the mineralization reactor (i.e., the waste heat from the gas in the carbon dioxide delivery pipeline 401), or it can be solar energy or other industrial waste heat, satisfying the requirement of "internal energy circulation".

[0081] The second solid-liquid separation structure 7 adopts a two-stage structure, consisting of a high-pressure plate and frame filter press and a second drying structure (hot air dryer). The filter cloth of the filter press is made of corrosion-resistant composite material. The high-pressure plate and frame filter press separates free water from the gelation products to obtain gelled wet material. The second drying structure (hot air dryer) dries the wet material to a suitable moisture content for storage. After drying, it is crushed into granular gelled material, forming the finished gelled material outlet 702. The finished gelled material outlet 702 is connected to the finished gelled material silo.

[0082] The high-pressure plate and frame filter press is connected to the extraction container 31 through the second filtrate delivery pipeline 701, and the filter filtrate is returned to the extraction tank for reuse, reducing wastewater discharge.

[0083] Based on the integrated closed-loop architecture of "pretreatment device 1 - carbon dioxide absorption device 2 - solid waste leaching device 3 - mineralization reaction device 4 - dual negative carbon product preparation device", this invention combines the quaternary material composition logic of "mixed amines (main absorbing amine + catalytic amine), synergistic leaching agent (acidic leaching + buffer), mineralization regulator (crystal inhibition + dispersion), and gelation activator (alkaline activation + coagulation regulation)" through the core steps of "amine non-thermal regeneration", "synergistic preparation of dual products" and "material / energy cycle", and adopts "multi-type solid waste + multi-industry flue gas" to simultaneously prepare nano-calcium carbonate and solid waste gelling materials, thereby improving the economic value and carbon emission reduction benefits of the system.

[0084] Furthermore, the pretreatment device 1 can be configured with different structures to accommodate different flue gases.

[0085] In one specific embodiment, the pretreatment device 1 adopts a three-stage series structure, including a cyclone separator, a bag filter and an alkaline spray tower. Each sub-component is connected by a flange, and each sub-component has a built-in airflow distribution plate.

[0086] A flue gas inlet is provided at the bottom of the pretreatment device 1, and an airflow distribution plate is provided above the flue gas inlet inside the pretreatment device 1; a pretreated flue gas outlet is provided at the top of the pretreatment device 1, and the pretreated flue gas outlet is connected to the bottom of the carbon dioxide absorption device 2 through a pretreated flue gas pipeline 101, which is a high-temperature resistant pipeline.

[0087] Pretreatment unit 1 is located at the very front of the system. The cyclone separator uses centrifugal force to separate coarse particulate impurities in the flue gas, making it suitable for high-dust flue gas. The bag filter traps fine particles through filter bags, ensuring that the packing of the subsequent absorption tower does not become clogged. The alkaline spray tower neutralizes SO2 / NO in the flue gas through alkaline liquid spraying. x To avoid amine degradation due to acidification.

[0088] The flue gas entering the system can be from steel / coal-fired power plants, or from chemical / cement plants, with a CO2 concentration of 8%-20%, and can be adapted to pretreatment processes.

[0089] The system for preparing negative carbon products through carbon dioxide capture and co-processing solid waste mineralization of the present invention includes multiple process links, including: (1) Flue gas treatment chain: Industrial flue gas → Pretreatment device 1 (cyclone separator → bag filter → alkaline spray tower) → bottom of carbon dioxide absorption device 2 (carbon dioxide absorption tower 21) → top of carbon dioxide absorption device 2 (carbon dioxide absorption tower 21) (emission in compliance with standards); (2) Amine liquid circulation link: Amine liquid at the bottom of carbon dioxide absorption device 2 → First circulation pump 2011 → Top of mineralization reaction device 4 (mineralization reactor) → Regenerated amine liquid inside mineralization reaction device 4 (mineralization reactor) → Second circulation pump 4031 → Top of carbon dioxide absorption device 2 (carbon dioxide absorption tower 21). (3) Mineralization-nano calcium carbonate link: Solid waste leaching device 3 (leaching tank) mixed liquid → leaching mixed liquid output pipeline 301 → mineralization reaction device 4 (mineralization reaction kettle) → nano calcium carbonate purification section (ceramic membrane → centrifugation → washing) → nano calcium carbonate finished product. (4) Cementitious material chain: Undissolved residue from solid waste extraction device 3 (extraction tank) → hydration reaction container 6 (pressurized reactor, with activator and residual heat heating) → second solid-liquid separation structure 7 (pressure filtration → drying) → finished cementitious material; (5) Carbon recovery chain: Unreacted CO2 at the top of mineralization reaction device 4 (mineralization reaction vessel) → carbon dioxide delivery pipeline 401 (second one-way valve 4011, i.e. CO2 reflux valve) → bottom of carbon dioxide absorption tower 21; (6) Material reuse chain: filtrate from the first solid-liquid separation structure 5 → solid waste leaching device 3 (leaching tank); filtrate from the second solid-liquid separation structure 7 → solid waste leaching device 3 (leaching tank); waste heat of unreacted CO2 (mineralization reactor tail gas) from mineralization reaction device 4 → hydration reaction heat exchange structure of cementitious material preparation section (hydration jacket of pressurized reactor). (7) Raw material supply chain: Absorbent liquid replenishment tank 22 → metering pump → top of carbon dioxide absorption tower 21; Solid waste material input section 32 (multi-source solid waste addition tank) → variable frequency screw conveyor → top of solid waste leaching device 3 (leaching tank).

[0090] This invention also provides a method for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization, implemented using the system of this invention; the method includes: The flue gas enters pretreatment unit 1 for pretreatment; The pretreated flue gas is fed into the carbon dioxide absorption device 2, and the composite amine liquid captures and absorbs the carbon dioxide in the pretreated flue gas to form a rich amine liquid; specifically, the pretreatment device 1 is connected to the carbon dioxide absorption device 2 to feed the pretreated flue gas into it, the carbon dioxide absorption device 2 is connected to the composite amine liquid input pipeline 202, and the composite amine liquid reacts with the carbon dioxide in the pretreated flue gas to form a rich amine liquid. Solid waste leaching device 3 connects the solid waste input section and the co-extractant input section. The co-extractant leaches the solid waste, dissolving the alkaline components (Ca) in the solid waste. 2+ / Mg 2+ After the alkaline components are extracted, the mixture is carried to the subsequent mineralization reaction unit 4 for further reaction; the extraction residue is output to the cementitious material preparation unit. Solid waste leaching device 3 contains alkaline components (Ca) from the solid waste material. 2+ / Mg 2+ The leaching mixture is output to the mineralization reaction device 4. The carbon dioxide absorption device 2 supplies the amine-rich solution to the mineralization reaction device 4 (mineralization reactor). Under the action of the mineralization regulator, the leaching mixture and the amine-rich solution undergo a mineralization reaction to generate a mineralized mixture containing nano-calcium carbonate. The regenerated amine solution and carbon dioxide gas are released through non-thermal amine regeneration. The carbon dioxide gas exchanges heat with the cementitious material preparation section and then returns to the carbon dioxide absorption device 2. The regenerated amine solution is output to the carbon dioxide absorption device 2 for reuse. Specifically, the solid waste leaching device 3 is connected to the mineralization reaction device 4 to input alkaline components (Ca) from the solid waste material. 2+ / Mg 2+The leaching mixture (carrying a small amount of leaching residue) is connected to the mineralization regulator input section of the mineralization reaction device 4. Under the action of the mineralization regulator, the leaching mixture and the amine-rich solution undergo a mineralization reaction to generate nano-calcium carbonate and non-thermal regeneration of amine. Carbon dioxide gas and regenerated amine solution are output to the carbon dioxide absorption device 2 for reuse. After mineralization, the mixed liquid is output to the nano-calcium carbonate purification unit to purify and produce nano-calcium carbonate product. The remaining filtrate after purification is returned to the solid waste leaching unit 3, and the residue intercepted after purification is output to the cementitious material preparation unit. The residue after the reaction (including leaching residue and mineralization purification residue) undergoes a hydration reaction in the cementitious material preparation section to generate finished cementitious material. The remaining filtrate after hydration is returned to the solid waste leaching unit 3.

[0091] In one specific embodiment, the method for preparing negative carbon products through carbon dioxide capture and co-processing solid waste mineralization includes the following steps: S1. Flue gas pretreatment (to meet subsequent absorption requirements): Specifically, the following steps are included: S11. Coarse particle separation: Industrial flue gas first enters the cyclone separator of pretreatment device 1. The inlet wind speed generates centrifugal force to separate coarse particles (such as dust and slag particles) from the flue gas. The separated coarse particles are periodically discharged from the bottom ash discharge port. S12. Fine Particle Retention: The flue gas after cyclone separation enters the bag filter dust collector, which retains fine particles with a diameter of ≤10μm. When the pressure difference of the filter bag reaches the set threshold, the pulse jet cleaning device automatically cleans the dust to ensure the air permeability of the filter bag. S13. Neutralization of Acidic Gases: The purified flue gas enters the alkaline scrubbing tower, where it comes into countercurrent contact with the alkaline solution sprayed from the top of the tower, neutralizing SO2 and NO in the flue gas. X For acidic gases, the pH of the spray solution is controlled within a suitable and neutral range by an online monitoring instrument to prevent acidic gases from entering the absorption tower and corroding the amine solution; S14. Flue gas conditioning: The flue gas after three-stage purification is cooled to a temperature range suitable for amine absorption by a heat exchanger (existing technology) (to avoid high temperature accelerating amine degradation), and the humidity is adjusted to ≤80%. Then, it is transported to the bottom of carbon dioxide absorption tower 21 by a fan (existing technology).

[0092] S2. Capture and absorb carbon dioxide to form an amine-rich solution: Specifically, the following steps are included: S21, Amine Liquid Preparation: The composite amine absorbent (main absorbing amine + catalytic amine) in the absorbent replenishment tank 22 is delivered to the top of the carbon dioxide absorption tower 21 by a metering pump, and then evenly sprayed onto the surface of the packing layer by a liquid distributor to form a uniform liquid film. S22, Gas-liquid contact: The pretreated flue gas enters from the bottom of the carbon dioxide absorption tower 21 and comes into countercurrent contact with the amine liquid film on the surface of the packing layer. The main absorbing amine in the amine liquid reacts chemically with CO2 in the flue gas to generate a rich amine liquid (containing carbamates). The catalytic amine increases the reaction rate through proton transfer, while inhibiting the degradation of the main absorbing amine. S23, Amine liquid circulation: The rich amine liquid in the bottom buffer zone of the carbon dioxide absorption tower 21 is transported to the mineralization reactor through the first circulation pump 2011 for subsequent non-thermal amine regeneration; when the concentration of amine liquid in the carbon dioxide absorption tower 21 decreases due to degradation / loss, the absorbent replenishment tank 22 automatically replenishes fresh amine liquid to maintain the amine liquid concentration within the range suitable for absorption efficiency. S24. Exhaust gas emission: Unabsorbed flue gas (mainly N2 and O2) is discharged from the top of carbon dioxide absorption tower 21. Before emission, the CO2 concentration is detected by an online monitoring instrument to ensure compliance (concentration ≤1%).

[0093] S3. Solid waste leaching (core coupling step): Specifically, the following steps are included: S31. Raw material input: Solid waste materials (such as steel slag / fly ash) in the multi-source solid waste addition tank are fed into the leaching tank through a variable frequency screw conveyor, and a co-extraction agent (acidic leaching component + buffer component) is added at the same time. The ratio of solid waste materials to co-extraction agent is controlled within the range suitable for leaching. S32. Synergistic reaction: The acidic component in the synergistic extractant dissolves Ca from the solid waste. 2+ / Mg 2+ S34, Material Diversion: The material in the extraction tank (extraction residue + post-extraction mixture) is divided into two paths: ① The extraction residue is transported to the cementitious material preparation section through residue pipeline 8; ② The material contains alkaline components (Ca) from the solid waste. 2+ / Mg 2+ The leaching mixture (carrying a small amount of leaching residue) is transported to the mineralization reactor through the first one-way valve 3011.

[0094] S4. Mineralization preparation of nano-calcium carbonate: Specifically, the following steps are included: S41. Mineralization reaction start-up: After leaching, the mixed solution and amine-rich solution are introduced into the mineralization reactor. A mineralization regulator (crystal growth inhibitor + dispersant) is added. The propeller-type agitator is stirred at high speed to promote uniform dispersion of the regulator. The leaching jacket is heated to the appropriate temperature range for mineralization to promote crystal growth. Ca in the mixture after extraction 2+ / Mg 2+ CO3 in amine-rich liquid 2-The reaction produces a calcium carbonate precursor (suspended in the mixed liquid); the carbamates in the amine-rich liquid decompose, releasing the regenerated amine liquid and CO2, achieving non-thermal amine regeneration without the need for high temperature and high pressure; the regenerated amine liquid is returned to the top of the carbon dioxide absorption tower 21 for reuse via the second circulation pump 4031. S42. Nanocrystal regulation: ① Crystal growth inhibitors are adsorbed on the surface of calcium carbonate precursors to limit crystal particle size growth to the nanoscale (≤100nm); ② Dispersants reduce solid-liquid interfacial tension and prevent the agglomeration of nano-calcium carbonate; ③ Online particle size monitors calcium carbonate particle size in real time on the side wall of the mineralization reactor and optimizes particle size by adjusting stirring speed / regulator dosage. S43. Unreacted CO2 recovery: Unreacted CO2 generated by the mineralization reaction is discharged from the top of the mineralization reactor and fed back to the bottom of the carbon dioxide absorption tower 21 through the second one-way valve 4011 (CO2 reflux valve) for secondary capture and utilization, thereby improving carbon utilization rate. S44. Primary separation: The mineralized mixture (nano-calcium carbonate + undissolved residue) is discharged from the bottom of the mineralization reactor and transported to the nano-calcium carbonate purification section.

[0095] Key implementation points for S3 and S4: Control the pH in the extraction tank within the Ca2+ range. 2+ / Mg 2+ The dissolution range (adjusted by the extraction buffer component) should be maintained to avoid excessively high pH levels leading to calcium loss. 2+ Precipitation; This invention is the first to combine "amine regeneration" with "solid waste extraction", eliminating the need for high-temperature equipment (such as desorption towers and steam boilers) in traditional amine thermal regeneration, and reducing system energy consumption.

[0096] S5, nano-calcium carbonate purification, ensuring product performance: Specifically, the following steps are included: S51. Coarse residue removal: After mineralization, the mixture first enters the ceramic membrane filter of the first solid-liquid separation structure 5. The membrane pore size is controlled within the range suitable for retaining coarse residue, and undissolved residue is retained (subsequently sent to a pressurized reactor to prepare gelling materials). The nano calcium carbonate suspension permeates through the ceramic membrane. S52. Centrifugal separation: The nano-calcium carbonate suspension that has passed through the membrane enters a disc centrifuge. The wet nano-calcium carbonate material and the mother liquor are separated by high-speed centrifugal force (separation factor ≥4000). The mother liquor is then transported to an extraction tank for reuse. S53. Washing and impurity removal: The wet nano-calcium carbonate material enters the countercurrent washing tower and is washed countercurrently with purified water (to remove residual regulators / amine liquid). The number of washing cycles is set according to the purity requirements of the product. After washing, the wet nano-calcium carbonate material is sent to the first drying structure (such as a vacuum dryer) to dry to a suitable moisture content for storage, thus obtaining the finished nano-calcium carbonate product.

[0097] S6. Preparation of cementitious materials from solid waste residue: Specifically, the following steps are included: S61. Residue conveying: The undissolved residue retained by the first solid-liquid separation structure 5 and the small amount of insoluble residue deposited at the bottom of the extraction tank are conveyed together to the pressurized reactor. S62. Addition of activator: The gelation activator (alkaline activating component + coagulation regulating component) is added from the top feed port of the pressurized reactor and mixed with the residue. The amount of activator is set according to the content of active components in the residue. S63. Waste Heat Utilization and Hydration Reaction: The hydration jacket is connected to the carbon dioxide delivery pipeline 401 (mineralization reactor tail gas pipeline). The waste heat of the mineralization tail gas (CO2 gas generated by the mineralization reaction) is used to heat the material in the pressurized reactor to a temperature range suitable for gelation. A paddle agitator promotes solid-liquid contact. The alkaline activating component activates the active SiO2 / Al2O3 in the residue to generate hydrated calcium silicate (the core of gelation strength). The setting regulating component controls the initial / final setting time of the gelling material to meet the subsequent molding requirements. S64. Cementitious material molding: The cementitious mixture after hydration reaction is transported to the second solid-liquid separation structure 7. First, free water is separated by a high-pressure plate and frame filter press (the filtrate is reused in the extraction tank) to obtain wet cementitious material. The wet material is dried in a hot air dryer until the moisture content is ≤10%, and then crushed by a crusher to a suitable particle size (≤5mm) to obtain the finished solid waste cementitious material.

[0098] Key implementation points of S5 and S6: Precise separation of "nano-calcium carbonate and residue" is achieved through the control of the ceramic membrane pore size of the first solid-liquid separation structure 5, preventing residue contamination and affecting the purity of calcium carbonate; the activity differences of different residues are adapted by adjusting the activator formula in the pressurized reactor. This invention breaks through the limitations of existing technologies that produce only "single products," simultaneously achieving the preparation of "high-value-added nanomaterials + bulk cementing materials," thus improving the economic benefits of the system.

[0099] This invention features a fully cyclical system that achieves zero emissions and energy savings, including: Material recycling: ① The filtrate from the first solid-liquid separation structure 5 / the second solid-liquid separation structure 7 is reused in the leaching tank; ② The regenerated amine liquid from the mineralization reactor is reused in the carbon dioxide absorption tower 21; ③ The unreacted CO2 generated in the mineralization reactor is reused in the carbon dioxide absorption tower 21. Energy cycle: Waste heat from the tail gas of the mineralization reactor is used for heating the pressurized reaction vessel; System monitoring and control: The control unit (PLC control system) monitors parameters such as temperature, pressure, liquid level, and particle size of each component in real time, and automatically adjusts the flow rate of each circulating pump, the replenishment amount of the metering pump, and the stirring speed of each agitator to ensure stable system operation.

[0100] The following verification of the feasibility of the integrated core concept of "CO2 capture-solid waste leaching-mineralization reaction-dual products" in this invention is carried out through multi-scenario adaptation. It is not limited to specific numerical parameters, but focuses on explaining the correlation between "solid waste / flue gas characteristics → process adjustment logic → effect matching".

[0101] Example 1: Co-treatment of high-calcium solid waste with high-concentration CO2 flue gas (verification of the "low-energy amine regeneration" approach)

[0102] 1. Adaptation Scenario Definition

[0103] (1) Solid waste type: High calcium industrial solid waste (such as steel slag, carbide slag, etc., CaO content ≥45%, moisture content ≤15%), no complicated pretreatment is required, just select conventional crushing / screening equipment according to particle size distribution (to meet the feeding requirements of subsequent leaching tanks); (2) Flue gas type: high-concentration CO2 industrial flue gas (such as flue gas from steel converters and lime kilns, with a CO2 volume fraction ≥12%, and impurities mainly consisting of dust and acidic gases); (3) Core verification objectives: the supporting role of alkaline components of solid waste in the non-thermal regeneration of amines, and the feasibility of directional preparation of dual products under high calcium conditions.

[0104] 2. Core Operation Logic

[0105] (1) Flue gas pretreatment: Based on the dust concentration and acid gas type in the flue gas, a combined purification method of "cyclone separation + bag filter + alkaline spray" is selected (the dust removal accuracy should be sufficient to prevent clogging of the subsequent absorption module, the acid gas removal rate should be ≥85%, and the stability of the amine absorbent should be guaranteed). (2) CO2 absorption: The "main absorbing amine + catalytic amine" composite amine system of this invention is adopted, and the circulation rate of amine liquid and the spraying intensity are adjusted according to the CO2 concentration of flue gas (to ensure that the outlet CO2 concentration is ≤1% and the loading of rich amine liquid meets the requirements of mineralization reaction). (3) Leaching-mineralization coupling (core step): High-calcium solid waste material and synergistic extractant (acidic leaching component + buffer component) are added to the extraction tank (stirred reaction tank) according to the principle of "liquid-to-solid ratio adapted to solid waste density," and the reaction temperature is controlled at a level "adapted to the calcium content of the solid waste." 2+ Within the range of "dissolution efficiency", no additional heating / pressurization is required; Amine regeneration is achieved by utilizing the alkalinity of solid waste (regeneration rate ≥95%), and the Ca dissolved during the leaching process is utilized. 2+ It undergoes a mineralization reaction with CO2 released during the regeneration of rich amine solution, and the calcium carbonate particle size is controlled to be in the nanoscale range by a mineralization regulator (crystal growth inhibitor + dispersant) (to meet the purity and dispersibility requirements of high-end industry applications). (4) Preparation of two products: The mineralized product is processed through the first solid-liquid separation structure 5 (a staged separation module adapted to the purification requirements of nanoparticles, such as a combination of filtration and centrifugation) to obtain nano-calcium carbonate product (purity ≥98%, uniformly dispersed). After leaching, the solid waste residue (leaching residue) is mixed with a gelling activator consisting of an alkaline activating component and a setting regulator. The reaction temperature and time are adjusted according to the activity of the residue to prepare a gelling material that meets the strength requirements of the construction / building materials industry (28-day compressive strength ≥30MPa). (5) Recycling: The filtrate generated by the first solid-liquid separation structure 5 (separation module), the non-thermal regenerated amine liquid in the mineralization reactor, and the waste heat from the mineralization process are recycled and reused according to the principle of "adapting to the load of the preceding module" (liquid recycling rate ≥90%, waste heat utilization rate ≥80%), verifying the energy consumption advantage of the integrated closed loop.

[0106] 3. Dimensions of Effect Verification

[0107] Energy consumption advantage: Compared with the traditional "amine thermal regeneration + pure CaO mineralization" process, the energy consumption of this embodiment is significantly reduced (reduction ≥25%), mainly due to the alkaline replacement of high-temperature desorption of solid waste, which verifies the energy-saving performance of the "amine non-thermal regeneration" approach; Solid waste utilization: Active components of high-calcium solid waste (Ca 2+ With a utilization rate of ≥90%, the residue is 100% converted into cementitious materials, and there is no solid waste landfill, thus verifying the concept of "full utilization of solid waste". Product value: Both products meet the corresponding industry application standards (nano-calcium carbonate meets the requirements of high-end fillers, and cementitious materials meet the strength requirements of general building materials), validating the "high-value products" approach.

[0108] Example 2: Co-treatment of low-calcium solid waste with medium-to-low concentration CO2 flue gas

[0109] 1. Adaptation Scenario Definition

[0110] Solid waste type: Low-calcium industrial solid waste (such as fly ash, red mud, etc., CaO content 30%-45%, may contain impurity ions such as Fe). 3+ Na + (large specific surface area) Flue gas type: Low to medium concentration CO2 flue gas (such as combined flue gas from coal-fired power plants and chemical industrial parks, with a CO2 volume fraction of 8%-12%, and impurities may include NO). X (VOCs, etc.) Core verification objective: To verify the adaptability of the present invention to non-ideal raw materials for process adjustment logic of low-calcium / high-impurity solid waste and low-concentration flue gas.

[0111] 2. Core Operation Logic

[0112] (1) Optimization of solid waste pretreatment: To address the characteristics of low-calcium solid waste, such as its large specific surface area and tendency to float / agglomerate, adjust the pretreatment method before impregnation (e.g., pre-stirring and mixing the slurry, adding a small amount of dispersant) to ensure sufficient solid-liquid contact; if it contains Fe... 3+ Na + To eliminate interfering ions, add appropriate impurity inhibitors (such as chelating agents and precipitants) to the extraction agent to avoid affecting the regeneration of the amine solution and the purity of the product. (2) Flue gas absorption adjustment: For low concentrations of CO2, optimize the ratio of the composite amine system (the proportion of the main absorbing amine can be appropriately increased) and the operating parameters of the absorption tower (such as extending the gas-liquid contact time and adjusting the spray density) to ensure that the CO2 capture efficiency meets the requirements of the mineralization reaction (the loading of the rich amine liquid reaches the threshold). (3) Adaptation of leaching-mineralization parameters: Because the solid waste has a low CaO content, the concentration of the extractant and the reaction time were adjusted (to suit the Ca content). 2+ Dissolution efficiency (ensuring sufficient raw materials for mineralization reaction), leaching temperature is controlled within a range that balances dissolution rate and energy consumption; Mineralization stage according to Ca² + Adjusting the CO2 inlet rate by concentration and fine-tuning the amount of mineralization regulator (to avoid Ca²⁺) + (Insufficient crystal growth), ensuring that the performance of nano-calcium carbonate products meets the standards; (4) Gelation activation and strengthening: To address the issue of low gelling activity in low-calcium residues, the gelling activator formulation was optimized (a small amount of highly active activating components could be added), and the hydration reaction conditions were adjusted (such as appropriately increasing the reaction temperature and extending the reaction time) to ensure that the strength of the gelling material meets the standards.

[0113] 3. Dimensions of Effect Verification

[0114] Compatibility: Low-calcium solid waste (Ca) 2+ The utilization rate is ≥85%, and the CO2 capture efficiency of medium and low concentration flue gas is ≥90%, which verifies the adaptability of the present invention to non-ideal raw materials. Impurity control: The impurity ion content in the product is ≤0.5%, and the degradation rate after 50 cycles of amine solution is ≤5%, verifying the effectiveness of the "impurity suppression" adjustment strategy; Economic feasibility: Although the pretreatment / parameter adjustment increases costs slightly, the value of the two products still covers the treatment costs, and the revenue is increased by ≥30% compared with existing low-calcium solid waste disposal technologies (such as landfill), which verifies the economic feasibility of the approach.

[0115] Example 3: Synergistic Treatment of Mixed Solid Waste and Multiple Pollutant Composite Flue Gas (Verification of the "Integrated Closed-Loop" Approach)

[0116] 1. Adaptation Scenario Definition

[0117] Solid waste type: Mixed industrial solid waste (such as steel slag + fly ash, red mud + phosphogypsum, etc., mixed in any proportion, with complex composition but total CaO content ≥35%). Flue gas type: Multi-pollutant complex flue gas (such as integrated flue gas from industrial parks, containing CO2, SO2, NO) X Dust, small amounts of VOCs, and CO2 volume fraction of 8%-15%); Core verification objectives: The ability of the integrated system of this invention to withstand "multi-raw material mixed input" and the stability of the internal circulation of materials / energy.

[0118] 2. Core Operation Logic

[0119] (1) Synergistic pretreatment of multiple raw materials: The mixing ratio of the mixed solid waste is adjusted according to the principle of "balancing CaO content and impurity distribution", and "graded crushing + unified slurry adjustment" is used for pretreatment (to avoid uneven leaching caused by the accumulation of single solid waste); the composite flue gas is purified in multiple stages by "dust removal + desulfurization + denitrification + VOCs adsorption" (the treatment efficiency of each stage is set according to the requirements of subsequent modules, such as VOCs removal rate ≥90% to protect the amine solution). (2) Full-process coordinated control: The absorption module dynamically adjusts the amine liquid circulation rate based on the real-time CO2 concentration of the flue gas (through linkage control via online monitoring instruments). The extraction module fine-tunes the extraction agent formulation based on the real-time composition of the mixed solid waste (periodic sampling and analysis) to ensure that Ca... 2+ Dissolution; The mineralization and gelation module is based on the characteristics of the products from the preceding process (such as the Ca content of the leachate). 2+ The operating parameters (concentration, residue activity) are adaptively adjusted without requiring shutdown for adjustment. (3) Strengthening the circulatory system: The filtrate, regenerated amine solution, and waste heat are allocated to the corresponding preceding modules according to the principle of "differentiated reuse" (e.g., high-purity filtrate is returned to the leaching tank, and low-purity filtrate is returned to the flue gas spray; waste heat is preferentially supplied to the cementitious material preparation department, i.e., the cementitious module). The circulation is kept stable through valve interlock control (to avoid interference between modules).

[0120] 3. Dimensions of Effect Verification

[0121] Closed-loop stability: After 30 days of continuous operation, the fluctuation of parameters of each module is ≤10%, the liquid recycling rate is ≥92%, and the waste heat utilization rate is ≥85%, verifying the anti-interference capability of the integrated closed loop. Mixed compatibility: The total utilization rate of mixed solid waste is 100%, and the emissions of composite flue gas pollutants all meet the standards (CO2 capture rate ≥88%, and other pollutants meet the national industrial emission standards), verifying the "multi-raw material compatibility" approach. Extensibility: No core equipment needs to be replaced; the invention can be adapted to mixed scenarios simply by fine-tuning process parameters and material formulations, thus verifying its potential for large-scale promotion.

[0122] Example 4: Adaptability verification under extreme conditions (verifying the "robustness of the approach")

[0123] 1. Adaptation Scenario Definition

[0124] Solid waste type: High moisture content / high impurity solid waste (such as wet fly ash with a moisture content ≥25%; phosphogypsum containing phosphorus / fluorine impurities); Flue gas type: Low temperature / high humidity CO2 flue gas (such as chemical condensate tail gas, temperature ≤40℃, relative humidity ≥80%, CO2 volume fraction 8%-10%). Core verification objective: To demonstrate the adaptability of the proposed invention under extreme raw material conditions and eliminate the limitation of "dependence on specific parameters".

[0125] 2. Core Operation Logic

[0126] (1) Enhanced solid waste pretreatment: High-moisture solid waste is first dewatered using conventional dewatering equipment (such as belt filter press or centrifugal dewatering) to reduce it to a suitable moisture content (to meet the solid-to-liquid ratio requirements); high-impurity solid waste is pre-washed / adsorbed before leaching to remove impurities (e.g., phosphogypsum is pre-washed with a weak alkaline solution to remove phosphorus, so as to avoid affecting the purity of the mineralized products). (2) Flue gas absorption adaptation: Low-temperature and high-humidity flue gas is first pretreated by "heating / demisting" (to avoid amine liquid dilution and equipment corrosion), and the gas velocity and spray temperature of the absorption tower are adjusted (to adapt to the amine absorption efficiency at low temperature and ensure that the amine-rich liquid load meets the standard). (3) Fault tolerance of core module parameters: Solid waste leaching unit 3 (leaching module) appropriately extends the reaction time to compensate for the low leaching efficiency of extreme solid waste; mineralization reaction unit 4 (mineralization module) adjusts the amount of regulator to offset the effect of low temperature on crystal growth; cementing material preparation unit (cementing module) optimizes the type of activator (such as selecting a fast-setting activating component) to adapt to possible insufficient activity problems.

[0127] 3. Dimensions of Effect Verification

[0128] Robustness: Under extreme conditions, Ca 2+ The utilization rate is ≥80%, the CO2 capture rate is ≥85%, and the performance of the two products still meets the basic application requirements (not high-end but compliant). The verification approach does not rely on "ideal raw materials". Economic viability: The additional treatment costs under extreme conditions (such as dehydration and demisting) can be covered by the value of the dual products, and the cost is reduced by ≥20% compared with existing extreme solid waste / flue gas treatment technologies (such as hazardous waste incineration and dilution emissions), thus verifying the practical value of the approach.

[0129] Common conclusions from the examples (strengthening the protection of ideas): Universality of the approach: All embodiments are based on the core ideas of the present invention, namely "integrated closed loop", "amine non-thermal regeneration" and "dual product synergy". The goal can be achieved simply by adapting the "solid waste / flue gas characteristics → process adjustment logic" without changing the system architecture and material system, proving that the approach is not limited to specific parameters; Technical barriers: Unlike existing technologies that rely on high-purity raw materials / specific parameters, this invention solves the industry pain points of "high energy consumption, low utilization rate and poor adaptability" through the idea of ​​"characteristic adaptation + closed-loop cycle". All embodiments verify the feasibility and advancement of this idea. Extension Boundaries: As long as the requirement of "solid waste containing alkaline components (Ca)" is met. 2+ / Mg 2+ The invention addresses the fundamental condition that "flue gas contains captureable CO2". Regardless of changes in the specific composition, concentration, moisture content, and other parameters of solid waste / flue gas, the invention can adapt to these conditions through its adjustment approach, thus broadening the scope of protection and application of the technical solution.

[0130] The above description is merely an illustrative embodiment of the present invention and is not intended to limit the scope of the invention. Any equivalent changes and modifications made by those skilled in the art without departing from the concept and principles of the present invention should fall within the scope of protection of the present invention.

Claims

1. A system for the co-production of carbon dioxide products through carbon dioxide capture and solid waste mineralization, characterized in that, include: A pretreatment device for pretreating flue gas; A carbon dioxide absorption device for absorbing and capturing carbon dioxide in a compound amine solution to generate a rich amine solution; The pretreatment device is connected to the bottom of the carbon dioxide absorption device; Solid waste leaching device for leaching solid waste materials to generate leaching residue and leaching mixture; A mineralization reaction device is used to generate a mineralized mixture containing nano-calcium carbonate through a mineralization reaction of the leaching mixture, and to release regenerated amine liquid through non-thermal amine regeneration. The solid waste leaching device is connected to the mineralization reaction device through a leaching mixture output pipeline; the bottom of the carbon dioxide absorption device is connected to the mineralization reaction device through a rich amine liquid output pipeline; and the mineralization reaction device is connected to the top of the carbon dioxide absorption device through a regenerated amine liquid pipeline. A dual-negative carbon product preparation device includes a nano-calcium carbonate purification section for purifying the mineralized mixture to produce nano-calcium carbonate, and a cementitious material preparation section for hydrating the residue after reaction under the action of a cementitious activator to produce a cementitious material. The mineralization reaction device is connected to the nano-calcium carbonate purification section through a mineralized mixture output pipeline. The solid waste leaching device and the nano-calcium carbonate purification section are connected to the cementitious material preparation section through a residue pipeline. The control unit is electrically connected to the pretreatment device, the carbon dioxide absorption device, the solid waste leaching device, the mineralization reaction device, and the dual negative carbon product preparation device.

2. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 1, characterized in that, The mineralization reaction device is connected to a carbon dioxide delivery pipeline for outputting carbon dioxide gas. The cementitious material preparation unit includes a hydration reaction heat exchange structure. The carbon dioxide delivery pipeline is connected to the bottom of the carbon dioxide absorption device after heat exchange through the hydration reaction heat exchange structure.

3. The system for carbon dioxide capture and synergistic solid waste mineralization to prepare negative carbon products as described in claim 2, characterized in that, The nano-calcium carbonate purification unit is connected to the solid waste leaching device through a first filtrate delivery pipeline for conveying the remaining filtrate after purification of the mineralized mixture, and the cementitious material preparation unit is connected to the solid waste leaching device through a second filtrate delivery pipeline for conveying the remaining filtrate after the hydration reaction.

4. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 3, characterized in that, The carbon dioxide absorption device includes a carbon dioxide absorption tower, and the pretreatment device is connected to the bottom of the carbon dioxide absorption tower through a pretreatment flue gas pipeline; the top of the carbon dioxide absorption tower is connected to a composite amine liquid input pipeline and a clean flue gas discharge pipeline, and an amine liquid buffer zone is set at the bottom of the carbon dioxide absorption tower.

5. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 4, characterized in that, The carbon dioxide absorption tower is a packed tower, and the inner cavity of the packed tower is layered with stepped ring packing. A liquid distributor is installed at the top of the inner cavity of the packed tower, and the composite amine liquid inlet pipeline is connected to the liquid distributor. An amine liquid buffer zone is installed at the bottom of the inner cavity of the packed tower. The pretreatment device is connected to the bottom of the packed tower, and the clean flue gas discharge pipeline is installed at the top of the packed tower.

6. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 4, characterized in that, The composite amine liquid input pipeline is connected to an absorbent replenishment tank for supplying composite amine liquid into the carbon dioxide absorption tower. A metering pump is installed at the bottom of the absorbent replenishment tank, and a liquid level monitor is installed at the top of the absorbent replenishment tank.

7. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 4, characterized in that, The solid waste leaching device includes an leaching container for leaching solid waste materials to generate leaching residue and leaching mixture. The leaching container is connected to the solid waste material input section and the co-extracting agent input section. The leaching container is connected to the mineralization reaction device through the leaching mixture output pipeline. The leaching container is connected to the cementitious material preparation section through the residue pipeline.

8. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 7, characterized in that, The extraction container is an extraction tank. An anchor-type agitator is installed inside the extraction tank and attached to the tank wall. The top of the extraction tank is connected to the solid waste input section and the co-extraction agent input section. One side of the extraction tank is connected to the extraction mixture output pipeline. A first one-way valve is installed on the extraction mixture output pipeline.

9. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 8, characterized in that, The solid waste input section is a multi-source solid waste addition tank. The inner cavity of the multi-source solid waste addition tank is equipped with a magnetic separation and impurity removal device. The bottom of the multi-source solid waste addition tank is equipped with a variable frequency screw conveyor, and the outlet of the variable frequency screw conveyor is connected to the top of the extraction tank.

10. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 8, characterized in that, The mineralization reaction apparatus includes a mineralization reaction container for generating a mineralized post-mineralized mixture containing nano-calcium carbonate through a mineralization reaction of the leaching mixture and for releasing regenerated amine liquid through non-thermal amine regeneration. The mineralization reaction container is connected to a mineralization regulator input section. The leaching container is connected to the mineralization reaction container through the leaching mixture output pipeline. The carbon dioxide absorption tower is connected to the mineralization reaction container through a rich amine liquid output pipeline. The mineralization reaction container is connected to the top of the carbon dioxide absorption tower through a regenerated amine liquid pipeline that allows the regenerated amine liquid to flow unidirectionally into the carbon dioxide absorption tower. A first circulation pump is installed on the rich amine liquid output pipeline. A second circulation pump is installed on the regenerated amine liquid pipeline. The mineralization reaction container is connected to the bottom of the carbon dioxide absorption tower through the carbon dioxide delivery pipeline.

11. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 10, characterized in that, The mineralization reaction container is a mineralization reactor, which is equipped with a propeller-type agitator. The top of the mineralization reactor is connected to the mineralization regulator input section, the extraction mixture output pipeline, and the amine-rich liquid output pipeline. The top of the mineralization reactor is also connected to the carbon dioxide delivery pipeline, which is equipped with a second one-way valve. The side wall of the mineralization reactor is equipped with a mineralization jacket for heating the reactor, and the mineralization jacket is equipped with a temperature control interface. The side wall of the mineralization reactor is equipped with an online particle size monitoring port.

12. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 11, characterized in that, The nano-calcium carbonate purification unit includes a first solid-liquid separation structure. The mineralization reaction container is connected to the first solid-liquid separation structure through the mineralized mixture output pipeline. The first solid-liquid separation structure includes, in sequence, a ceramic membrane filter for retaining coarse residue in the mineralized mixture and for preliminarily purifying the nano-calcium carbonate suspension, a disc centrifuge for centrifugally separating the nano-calcium carbonate wet material from the mother liquor, a countercurrent washing tower for washing the nano-calcium carbonate wet material with purified water, and a first drying structure for drying the nano-calcium carbonate wet material. The ceramic membrane filter is connected to the cementitious material preparation unit through a residue pipeline. The disc centrifuge is connected to the extraction container through the first filtrate delivery pipeline. The first drying structure is provided with a nano-calcium carbonate finished product outlet.

13. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 12, characterized in that, The gelling material preparation unit includes a hydration reaction container, which is connected to a gelling activator input unit. The extraction container and the first solid-liquid separation structure are connected to the hydration reaction container through a residue pipeline. The hydration reaction heat exchange structure is provided on the hydration reaction container. The hydration reaction containment is connected to the second solid-liquid separation structure, which includes a high-pressure plate and frame filter press for separating the gelled wet material and free water in the hydration reaction products, and a second drying structure for drying the gelled wet material, which are connected in sequence. The high-pressure plate and frame filter press is connected to the extraction containment through the second filtrate conveying pipeline, and the second drying structure is provided with a finished gelled material outlet.

14. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 13, characterized in that, The hydration reaction container is a pressurized reactor. The top of the pressurized reactor is connected to the gelling activator input section and the residue pipeline. A paddle stirrer is installed in the inner cavity of the pressurized reactor. The hydration reaction heat exchange structure is a hydration jacket installed on the side wall of the pressurized reactor. The hydration jacket is connected to the carbon dioxide delivery pipeline. The bottom of the pressurized reactor is connected to the second solid-liquid separation structure.

15. The system for carbon dioxide capture and co-processing solid waste mineralization to prepare negative carbon products as described in claim 1, characterized in that, The pretreatment device includes a cyclone separator, a bag filter, and an alkaline spray tower. The bottom of the pretreatment device is provided with a flue gas inlet, and the top of the pretreatment device is provided with a pretreated flue gas outlet. The pretreated flue gas outlet is connected to the bottom of the carbon dioxide absorption device through a pretreated flue gas pipeline.

16. A method for preparing negative carbon products through carbon dioxide capture and synergistic solid waste mineralization, characterized in that, The system for preparing negative carbon products by carbon dioxide capture and synergistic solid waste mineralization as described in any one of claims 1-15 is adopted; The method for preparing negative carbon products by carbon dioxide capture and synergistic solid waste mineralization includes: The flue gas enters the pretreatment unit for pretreatment; The pretreated flue gas is fed into a carbon dioxide absorption device, where a composite amine solution captures and absorbs the carbon dioxide in the pretreated flue gas, forming a rich amine solution. The solid waste leaching device connects the solid waste material input section and the co-extracting agent input section. The co-extracting agent leaches the solid waste material, dissolving the alkaline components in the solid waste material. The alkaline components are carried by the leached mixture to the mineralization reaction device. The leaching residue is output to the cementitious material preparation section. The leaching mixture containing alkaline components from the solid waste material in the solid waste leaching unit is output to the mineralization reaction unit. The carbon dioxide absorption unit supplies amine-rich solution to the solid waste leaching unit. Under the action of the mineralization regulator, the amine-rich solution reacts with the leaching mixture to generate a mineralized mixture containing nano-calcium carbonate. The regenerated amine solution and carbon dioxide gas are released through non-thermal amine regeneration. The carbon dioxide gas exchanges heat with the cementitious material preparation unit and then returns to the carbon dioxide absorption unit; the regenerated amine solution returns to the carbon dioxide absorption unit. After mineralization, the mixed liquid is output to the nano-calcium carbonate purification unit to be purified into nano-calcium carbonate product. The remaining filtrate after purification is returned to the solid waste leaching unit, and the residue intercepted after purification is output to the cementitious material preparation unit. The leaching residue and the purified intercepted residue undergo a hydration reaction in the cementitious material preparation section to generate the finished cementitious material. The remaining filtrate after hydration is returned to the solid waste leaching unit.

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