Method for carbon dioxide mineralization and carbon dioxide mineralization device

Abstract

The present application relates to a kind of carbon dioxide mineralization method and carbon dioxide mineralization device.The carbon dioxide mineralization method includes the following steps: mixing absorption liquid and industrial solid waste at room temperature, obtain mortar;Make mortar solid-liquid separation, obtain clear liquid and thick slurry;Carbon dioxide in flue gas is absorbed by clear liquid, obtain carbon-rich absorption liquid;Carbon-rich absorption liquid and thick slurry occur mineralization reaction at 180 DEG C-220 DEG C, obtain mineralized slurry;Make mineralized slurry solid-liquid separation, obtain mineralized ash and mineralized clear liquid;Wherein, absorption liquid includes inorganic base and organic base, organic base includes monoethanolamine, diethanolamine, triethanolamine, 3-methylaminopropylamine, N-methyl diethanolamine, piperazine, diethylene triamine, triethylene tetramine, tetraethylene pentamine and 2-amino-2-methyl-1-propanolamine at least two kinds.The method greatly improves CO2 capture rate and CO2 utilization rate, and organic base consumption is less, absorption liquid regeneration energy consumption is low, and overall economy is good.

Description

Technical Field

[0001] This invention relates to the technical field of carbon dioxide emission reduction, and in particular to a method and apparatus for carbon dioxide mineralization. Background Technology

[0002] With the massive use of fossil fuels by humankind, large amounts of carbon dioxide (CO2) are emitted into the atmosphere, severely impacting the Earth's climate and ecosystem balance. Therefore, reducing CO2 emissions has become a widespread concern.

[0003] Currently, a key approach to CO2 emission reduction is carbon capture and storage (CCS) technology. This involves separating CO2 emitted from industrial emissions using carbon capture technology, and then using carbon storage technology to transport and store the CO2 on the seabed or underground. However, CCS technology carries the risk of CO2 escape, and suffers from low CO2 capture and utilization rates, high consumption of organic alkalis, and high energy consumption for absorbent regeneration, resulting in poor overall economic efficiency. Summary of the Invention

[0004] Therefore, it is necessary to provide a method and apparatus for carbon dioxide mineralization to solve problems such as low CO2 capture rate and CO2 utilization rate, large consumption of organic alkali, high energy consumption for absorbent regeneration, and poor overall economic efficiency.

[0005] The above-mentioned objective of this invention is achieved through the following technical solution:

[0006] In a first aspect, the present invention provides a method for carbon dioxide mineralization, comprising the following steps:

[0007] The absorbent liquid and industrial solid waste were mixed at room temperature to obtain mortar;

[0008] The mortar is separated into solid and liquid components to obtain a clear liquid and a concentrated mortar.

[0009] The clear liquid is used to absorb carbon dioxide from the flue gas to obtain a carbon-rich absorbent liquid.

[0010] The carbon-rich absorbent and the concentrated slurry are subjected to a mineralization reaction at 180°C to 220°C to obtain a mineralized slurry.

[0011] The mineralized slurry is subjected to solid-liquid separation to obtain mineralized ash residue and mineralized clear liquid;

[0012] The absorbent liquid comprises an inorganic base and an organic base, wherein the organic base comprises at least two of monoethanolamine, diethanolamine, triethanolamine, 3-methylaminopropylamine, N-methyldiethanolamine, piperazine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, and 2-amino-2-methyl-1-propanolamine.

[0013] In one embodiment, the organic base is monoethanolamine and piperazine.

[0014] In one embodiment, the organic base is present in the absorbent at a concentration of 4 wt.% to 12 wt.%.

[0015] In one embodiment, the organic base satisfies one or more of the following conditions:

[0016] 1) The content of the monoethanolamine in the absorbent is 2 wt.% to 8 wt.%;

[0017] 2) The content of the piperazine in the absorbent is 2 wt.% to 4 wt.%.

[0018] In one embodiment, the inorganic base satisfies one or more of the following conditions:

[0019] 1) The content of the inorganic base in the absorption liquid is 20 wt.% to 25 wt.%;

[0020] 2) The inorganic base includes one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, potassium carbonate and sodium phosphate.

[0021] In one embodiment, the step of mixing the absorbent and the industrial solid waste satisfies one or more of the following conditions:

[0022] 1) The liquid-to-solid ratio of the absorbent to the industrial solid waste is 1L:(1kg~1.2kg);

[0023] 2) The time for mixing the absorbent and the industrial solid waste is 0.5h to 1h.

[0024] In one embodiment, the step of causing the clarified liquid to absorb carbon dioxide from the flue gas satisfies one or more of the following conditions:

[0025] 1) The gas velocity of the flue gas is 2m / s to 3m / s;

[0026] 2) The temperature of the flue gas is 35℃~45℃;

[0027] 3) The carbon dioxide concentration in the flue gas is 200 g / Nm³. 3 ~300g / Nm 3 ;

[0028] 4) The liquid-to-gas ratio of the clarified liquid to the flue gas is (1L~1.5L):1m 3 .

[0029] In one embodiment, the mineralization reaction satisfies one or more of the following conditions:

[0030] 1) The reaction pressure of the mineralization reaction is 1.0 MPa to 2.0 MPa;

[0031] 2) The reaction time for the mineralization reaction is 1 to 2 hours;

[0032] 3) The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry is (2-3):1.

[0033] In one embodiment, the industrial solid waste meets one or more of the following conditions:

[0034] 1) The calcium oxide content of the industrial solid waste is ≥10 wt.%.

[0035] 2) The particle size of the industrial solid waste is ≤75μm;

[0036] 3) The industrial solid waste includes one or more of the following: fly ash, steel slag, carbide slag, waste cement, and waste gypsum.

[0037] In a second aspect, the present invention provides a carbon dioxide mineralization apparatus, comprising a slurry mixing tank, a slurry separator, an absorption tower, a mineralization reactor, and a mineralization slurry separator connected in sequence by pipelines, wherein the slurry separator and the mineralization reactor are connected by pipelines.

[0038] The present invention has the following beneficial effects:

[0039] First, compared with traditional high-temperature pretreatment methods, mixing the absorbent and industrial solid waste at room temperature is a simple, easy, economical, and effective pretreatment method. During the mixing process, the absorbent washes away toxic heavy metal ions and extremely fine particulate matter from the industrial solid waste and dissolves some alkaline active substances. This reduces the alkalinity and heavy metal content of the industrial solid waste and enhances the CO2 capture capacity of the subsequent clarified liquid. Simultaneously, the absorbent fully wets the industrial solid waste and penetrates its porous structure, forming a liquid film on its inner and outer surfaces. This liquid film facilitates interfacial transport and reaction, activating the industrial solid waste and accelerating the mineralization reaction rate.

[0040] Secondly, the multi-component mixed absorbent obtained by combining an inorganic base with at least two organic bases that have a strong affinity for CO2 significantly reduces the feed amount and regeneration energy consumption of the absorbent. Furthermore, it has a larger CO2 absorption capacity and a faster absorption rate, and also promotes the dissolution of calcium-containing compounds in the solution, greatly improving the CO2 capture and mineralization efficiency. Primary and secondary amines such as MEA, DEA, and PZ can react with CO2 to form carbamates and protonated amines, with reaction rates faster than the hydration of CO2 or the reaction rate between CO2 and inorganic bases. Tertiary amines such as TEA and AMP, and sterically hindered amines, can capture protons, thereby accelerating the hydration of CO2 or the reaction rate between CO2 and inorganic bases.

[0041] Furthermore, by subjecting the carbon-rich absorbent liquid and concentrated slurry to a mineralization reaction at 180℃~220℃ followed by solid-liquid separation, CO2 can be directly encapsulated in industrial solid waste, significantly reducing the alkalinity and heavy metal ion content of the industrial solid waste and obtaining mineralized ash slag with high added value and low environmental hazard. Simultaneously, the carbon-rich absorbent liquid is regenerated into a mineralized clear liquid that can be used as an absorbent liquid, exhibiting a higher CO2 desorption rate, lower energy consumption for absorbent liquid regeneration, and a higher recycling rate, while avoiding the risk of CO2 leakage and escape.

[0042] In summary, the CO2 mineralization system of the present invention can significantly improve the CO2 capture rate and CO2 utilization rate, and has low organic alkali consumption, low energy consumption for absorbent regeneration, and good overall economic efficiency. It is conducive to the integration of CO2 capture, utilization and storage, as well as the resource utilization of industrial solid waste, and has great economic and environmental benefits. Attached Figure Description

[0043] Figure 1 This is a schematic diagram of a carbon dioxide mineralization device according to an embodiment of the present invention.

[0044] Reference numerals: 11. Absorbent liquid storage tank; 12. Absorbent liquid pump; 13. Ash silo; 14. Screw feeder; 15. Mortar mixing tank; 16. Mortar pump; 17. Mortar hydrocyclone; 18. Thick slurry tank; 19. Clear liquid storage tank; 21. Cooling water pump; 22. Washing tower; 22a. Nozzle; 23. Exhaust fan; 24. Clear liquid pump; 25. Clear liquid cooler; 26. Absorbent tower; 26a. Nozzle; 27. Circulating pump; 28. Carbon-rich absorbent liquid cooler; 31. Carbon-rich absorbent liquid pump; 32. Heat exchanger; 33. Thick slurry pump; 34. Mineralization reactor; 35. Mineralization slurry pump; 36. Mineralization slurry hydrocyclone; 37. Vacuum belt dewatering machine. Detailed Implementation

[0045] To make the above-mentioned objects, features, and advantages of the present invention more apparent and understandable, specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of the present invention. However, the present invention can be practiced in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.

[0046] 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 invention pertains. The terminology used herein in the specification of this invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0047] Of the CO2 emitted by human activities, thermal power plants account for more than 30% of global carbon emissions. With the development of carbon reduction technologies, coal-fired industries, including thermal power plants, are facing technological choices regarding carbon reduction. However, the currently widely used CCS (Carbon Capture and Storage) technology is too costly, has low CO2 capture and utilization rates, and carries a high risk of CO2 leakage, making it unfavorable for achieving green and energy-saving carbon reduction goals.

[0048] Meanwhile, fly ash produced from coal combustion in thermal power plants is also a major source of industrial solid waste. Large quantities of untreated fly ash can lead to severe environmental pollution and harm to organisms. Currently, only 56% of fly ash production is utilized for resource recovery, primarily for road paving, mine backfilling, and as an admixture in cement, mortar, and concrete. However, fly ash has high water absorption, low strength, is easily weathered, and retains toxic heavy metal ions, all of which hinder its resource utilization.

[0049] Therefore, improving the CO2 capture and utilization rate of carbon emission reduction technologies and realizing the high-value utilization of industrial solid wastes such as fly ash has become the most attention-grabbing topic in the field of environmental protection.

[0050] Based on this, in a first aspect, the present invention provides a method for carbon dioxide mineralization, comprising the following steps:

[0051] The absorbent liquid and industrial solid waste were mixed at room temperature to obtain mortar;

[0052] The mortar is separated into solid and liquid components to obtain a clear liquid and a concentrated mortar.

[0053] The clear liquid is used to absorb carbon dioxide from the flue gas to obtain a carbon-rich absorbent liquid.

[0054] The carbon-rich absorbent and the concentrated slurry are subjected to a mineralization reaction at 180°C to 220°C to obtain a mineralized slurry.

[0055] The mineralized slurry is subjected to solid-liquid separation to obtain mineralized ash residue and mineralized clear liquid;

[0056] The absorbent liquid comprises an inorganic base and an organic base, wherein the organic base comprises one or more of monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA), 3-methylaminopropylamine, N-methyldiethanolamine (MDEA), piperazine (PZ), diethylenetriamine (DETA), triethylenetetramine (TETA), tetraethylenepentamine (TEPA), and 2-amino-2-methyl-1-propanolamine (AMP).

[0057] Understandably, the room temperature is normal or general temperature, with a temperature range of 20℃ to 30℃.

[0058] Understandably, the industrial solid waste refers to solid waste generated in industrial production activities such as metallurgy and thermal power generation, including fly ash, steel slag, blast furnace slag, carbide slag, red mud, waste cement, waste gypsum, desulfurization ash, etc.

[0059] Understandably, the solvent of the absorbent is water, that is, an inorganic base and an organic base are dissolved in water and stirred evenly to obtain the absorbent.

[0060] First, compared with traditional high-temperature pretreatment methods, mixing the absorbent and industrial solid waste at room temperature is a simple, easy, economical, and effective pretreatment method. During the mixing process, the absorbent washes away toxic heavy metal ions and extremely fine particulate matter from the industrial solid waste and dissolves some alkaline active substances. This reduces the alkalinity and heavy metal content of the industrial solid waste and enhances the CO2 capture capacity of the subsequent clarified liquid. Simultaneously, the absorbent fully wets the industrial solid waste and penetrates its porous structure, forming a liquid film on its inner and outer surfaces. This liquid film facilitates interfacial transport and reaction, activating the industrial solid waste and accelerating the mineralization reaction rate.

[0061] Secondly, the multi-component mixed absorbent obtained by combining an inorganic base with at least two organic bases that have a strong affinity for CO2 significantly reduces the feed amount and regeneration energy consumption of the absorbent. Furthermore, it has a larger CO2 absorption capacity and a faster absorption rate, and also promotes the dissolution of calcium-containing compounds in the solution, greatly improving the CO2 capture and mineralization efficiency. Primary and secondary amines such as MEA, DEA, and PZ can react with CO2 to form carbamates and protonated amines, with reaction rates faster than the hydration of CO2 or the reaction rate between CO2 and inorganic bases. Tertiary amines such as TEA and AMP, and sterically hindered amines, can capture protons, thereby accelerating the hydration of CO2 or the reaction rate between CO2 and inorganic bases.

[0062] Furthermore, by subjecting the carbon-rich absorbent liquid and concentrated slurry to a mineralization reaction at 180℃~220℃ followed by solid-liquid separation, CO2 can be directly encapsulated in industrial solid waste, significantly reducing the alkalinity and heavy metal ion content of the industrial solid waste and obtaining mineralized ash slag with high added value and low environmental hazard. Simultaneously, the carbon-rich absorbent liquid is regenerated into a mineralized clear liquid that can be used as an absorbent liquid, exhibiting a higher CO2 desorption rate, lower energy consumption for absorbent liquid regeneration, and a higher recycling rate, while avoiding the risk of CO2 leakage and escape.

[0063] In summary, the CO2 mineralization system of the present invention can significantly improve the CO2 capture rate and CO2 utilization rate, and has low organic alkali consumption, low energy consumption for absorbent regeneration, and good overall economic efficiency. It is conducive to the integration of CO2 capture, utilization and storage, as well as the resource utilization of industrial solid waste, and has great economic and environmental benefits.

[0064] In some preferred embodiments, the content of the organic base in the absorbent is lower than the content of the inorganic base.

[0065] In some preferred embodiments, the method for solid-liquid separation of the mineralized slurry and the method for solid-liquid separation of the ash slurry are cyclone separation methods, and the separation particle size of the cyclone separation method is 50 μm.

[0066] Solid particles smaller than 50 μm remain in the clear liquid and mineralized clear liquid, and help the clear liquid seal CO2 during the CO2 absorption process, thereby increasing the amount of CO2 fixed.

[0067] In some preferred embodiments, the step of solid-liquid separation of the mineralized slurry is to cool the mineralized slurry to below 100°C and then perform solid-liquid separation.

[0068] When cooled to 100℃, the water will change from a gaseous state to a liquid state, which can redissolve the inorganic and organic bases in the mineralized slurry, thus facilitating the regeneration of the absorbent.

[0069] In some preferred embodiments, the step of recovering the mineralized solution and continuing to use it as the solution is further included.

[0070] In some preferred embodiments, the step of recovering a portion of the clarified liquid and continuing to use it as the absorbent is further included.

[0071] The clear liquid and mineralized clear liquid contain organic alkali, inorganic alkali, various eluted ions and extremely fine particulate matter. Recovering the excess clear liquid for use as an absorbent and the mineralized clear liquid for use as a clear liquid helps to reduce the operating cost of the CO2 mineralization system.

[0072] In some embodiments, the organic base is monoethanolamine and piperazine.

[0073] Taking MEA(HOCH2CH2NH2) as an example, its specific reaction is as follows:

[0074]

[0075] The addition of MEA and PZ to the absorbent greatly accelerates the CO2 dissolution rate and CO2 solubility in the solution, and enhances the solubility of mineral products such as calcium-containing compounds, thus preventing calcium-containing compounds from covering the surface of industrial solid waste and affecting the smooth progress of the mineralization reaction.

[0076] In some embodiments, the organic base in the absorbent is present in an amount of 4 wt.% to 12 wt.%.

[0077] The low content of organic bases in the absorbent reduces the oxidative degradation of organic bases in the mineralization reaction, further reducing the energy consumption for regeneration of the absorbent and also reducing corrosion to instruments and equipment.

[0078] In some embodiments, the organic base satisfies one or more of the following conditions:

[0079] 1) The content of the monoethanolamine in the absorbent is 2 wt.% to 8 wt.%;

[0080] 2) The content of the piperazine in the absorbent is 2 wt.% to 4 wt.%.

[0081] By adjusting the content of different components in the absorbent, the absorption capacity of the absorbent for CO2 can be improved, the amount of absorbent fed and consumed can be reduced, thereby improving the economic efficiency of the CO2 mineralization system.

[0082] In some preferred embodiments, the content of the monoethanolamine in the absorbent is 4 wt.% to 8 wt.%, and the content of the piperazine in the absorbent is 2 wt.% to 3 wt.%.

[0083] In some preferred embodiments, the monoethanolamine is present in an amount of 8 wt.% in the absorbent, and the piperazine is present in an amount of 2 wt.% in the absorbent.

[0084] In some embodiments, the inorganic base satisfies one or more of the following conditions:

[0085] 1) The content of the inorganic base in the absorption liquid is 20 wt.% to 25 wt.%;

[0086] 2) The inorganic base includes one or more of sodium hydroxide (NaOH), potassium hydroxide (KOH), sodium carbonate (Na2CO3), potassium carbonate (K2CO3), and sodium phosphate (Na3PO4).

[0087] Inorganic alkalis have good CO2 capture capacity, and the raw materials are inexpensive. They do not undergo oxidative degradation during mineralization reactions, and the regeneration energy consumption is low.

[0088] In some preferred embodiments, the inorganic base includes NaOH and / or Na2CO3.

[0089] In some preferred embodiments, the inorganic base is Na2CO3.

[0090] In some preferred embodiments, the inorganic base in the absorbent is present in an amount of 20 wt.% to 22 wt.%.

[0091] In some preferred embodiments, the inorganic base in the absorbent is present in an amount of 20 wt.%.

[0092] In some embodiments, the step of mixing the absorbent and the industrial solid waste satisfies one or more of the following conditions:

[0093] 1) The liquid-to-solid ratio of the absorbent to the industrial solid waste is 1L:(1kg~1.2kg);

[0094] 2) The time for mixing the absorbent and the industrial solid waste is 0.5h to 1h.

[0095] By selecting appropriate feeding ratios and mixing times based on the types and contents of effective components in the absorbent and the particle size and composition of industrial solid waste, most heavy metal ions and fine particulate matter in industrial solid waste can be washed away, and the industrial solid waste can be fully wetted and activated, thereby increasing CO2 absorption efficiency and mineralization efficiency, and reducing the environmental pollution of mineralization products.

[0096] In some preferred embodiments, the time for mixing the absorbent and the industrial solid waste is 1 hour.

[0097] In some embodiments, the step of having the clarified liquid absorb carbon dioxide from the flue gas satisfies one or more of the following conditions:

[0098] 1) The gas velocity of the flue gas is 2m / s to 3m / s;

[0099] 2) The temperature of the flue gas is 35℃~45℃;

[0100] 3) The carbon dioxide concentration in the flue gas is 200 g / Nm³. 3 ~300g / Nm 3 ;

[0101] 4) The liquid-to-gas ratio of the clarified liquid to the flue gas is (1L~1.5L):1m 3 .

[0102] Understandably, the gas velocity is the flow rate of the gas, also known as the unit volume flow rate, which represents the speed or amount of movement of a unit volume of gas particles per unit time. In plate towers or packed towers used in gas absorption operations, the average flow rate of the gas through the tower is generally calculated based on an empty tower, and the gas velocity is obtained by dividing the gas flow rate by the total cross-sectional area of ​​the fluidized bed.

[0103] Adjusting parameters such as the volume ratio of flue gas to clarified liquid, the gas velocity of flue gas, and the temperature of flue gas can improve the dissolution rate and solubility of CO2 in clarified liquid, allowing CO2 in flue gas to be fully absorbed by clarified liquid, thereby improving the CO2 capture rate.

[0104] In some embodiments, the mineralization reaction satisfies one or more of the following conditions:

[0105] 1) The reaction pressure of the mineralization reaction is 1.0 MPa to 2.0 MPa;

[0106] 2) The reaction time for the mineralization reaction is 1 to 2 hours;

[0107] 3) The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry is (2-3):1.

[0108] The carbon-rich absorbent obtained after CO2 absorption by the clarified liquid contains bicarbonate or hydrogen phosphate, carbamate, and protonated amine. Taking Na2CO3 and MEA as examples, the carbon-rich absorbent will react with the mortar under high temperature and pressure as follows:

[0109]

[0110]

[0111]

[0112]

[0113]

[0114] Therefore, the mineralization reaction not only generates high-value-added carbonate precipitates but also regenerates the carbon-rich absorbent into a recyclable mineralized solution. Furthermore, the presence of organic amines promotes the dissolution of carbonate precipitates covering the surface of industrial solid waste, preventing precipitates from hindering the reaction and significantly reducing the energy consumption of absorbent regeneration while also significantly improving CO2 utilization. In addition, selecting an appropriate feed ratio can improve the mineralization efficiency of both CO2 and fly ash.

[0115] In some preferred embodiments, the volume ratio of the carbon-rich absorbent to the concentrated slurry is 3:1.

[0116] In some embodiments, the industrial solid waste meets one or more of the following conditions:

[0117] 1) The calcium oxide content of the industrial solid waste is ≥10 wt.%.

[0118] 2) The particle size of the industrial solid waste is ≤75μm;

[0119] 3) The industrial solid waste includes one or more of the following: fly ash, steel slag, carbide slag, waste cement, and waste gypsum.

[0120] Among various industrial solid wastes, fly ash, steel slag, blast furnace slag, red mud, carbide slag, and desulfurization ash contain a significant amount of calcium oxide, which can be used for CO2 mineralization and sequestration. The higher the calcium oxide content and the smaller the particle size of the industrial solid waste, the higher its reactivity, the higher its mineralization efficiency, and the better its economic benefits.

[0121] In some preferred embodiments, the calcium oxide content of the industrial solid waste is ≥20 wt.%.

[0122] In some preferred embodiments, the industrial solid waste is fly ash.

[0123] Fly ash has advantages such as small particle size, high reactivity, and proximity to CO2 emission sources, making it more suitable for CO2 mineralization in coal-fired industries such as thermal power plants.

[0124] In a second aspect, the present invention provides a carbon dioxide mineralization apparatus, comprising a slurry mixing tank, a slurry separator, an absorption tower, a mineralization reactor, and a mineralization slurry separator connected in sequence by pipelines, wherein the slurry separator and the mineralization reactor are connected by pipelines.

[0125] In some preferred embodiments, the slurry separator is a slurry hydrocyclone, and the mineralized slurry separator is a mineralized slurry hydrocyclone.

[0126] In some preferred embodiments, the separation particle size of the slurry hydrocyclone and the mineralized slurry hydrocyclone is 50 μm.

[0127] In some preferred embodiments, the absorption tower is a spray tower.

[0128] In some preferred embodiments, the top of the absorption tower is provided with nozzles and a demister.

[0129] In some preferred embodiments, the mineralization reactor is provided with a heating jacket on the outside and a stirrer, thermometer and level gauge inside.

[0130] In some preferred embodiments, the carbon dioxide mineralization device includes a pretreatment unit, a carbon dioxide absorption unit, and a mineralization reaction unit;

[0131] The pretreatment unit includes an absorbent storage tank, an absorbent pump, a slurry mixing tank, a slurry pump, and a slurry hydrocyclone connected in sequence by pipelines, a screw feeder installed above the slurry mixer, an ash silo installed above the screw feeder, a clear liquid storage tank connected at one end to the slurry hydrocyclone and at the other end to the carbon dioxide absorption unit by a pipeline, and a concentrated slurry tank connected at one end to the slurry hydrocyclone and at the other end to the mineralization reaction unit by a pipeline;

[0132] The carbon dioxide absorption unit includes a cooling water pump, a water washing tower, an induced draft fan, and an absorption tower connected in sequence by pipelines, a clear liquid pump connected to the clear liquid storage tank by pipelines, and a clear liquid cooler connected at one end to the clear liquid pump and at the other end to the absorption tower by pipelines. The absorption tower is connected to the mineralization reaction unit by pipelines.

[0133] The mineralization reaction unit includes a carbon-rich absorbent pump, a heat exchanger, a mineralization reactor, a mineralization slurry pump, a mineralization slurry hydrocyclone, and a vacuum belt dewatering machine, which are connected in sequence by pipelines. It also includes a slurry pump that is connected at one end to the slurry tank and at the other end to the mineralization reactor by a pipeline. The carbon-rich absorbent pump is connected to the absorption tower by a pipeline.

[0134] In some preferred embodiments, the clear liquid storage tank and the mortar mixing tank are connected by a pipeline.

[0135] In some preferred embodiments, the carbon dioxide absorption unit further includes a circulation pump connected to the absorption tower via a pipeline and a carbon-rich absorbent cooling pump connected at one end to the circulation pump and at the other end to the absorption tower via a pipeline.

[0136] The present invention will be further described in detail below with reference to specific embodiments.

[0137] Example 1

[0138] Please refer to Table 1. The absorbent in this embodiment contains 20 wt.% Na2CO3, 8 wt.% MEA and 2 wt.% PZ, and the industrial solid waste is fly ash with a CaO content of 25%.

[0139] (1) Preprocessing unit

[0140] Please see Figure 1 The prepared absorbent solution is stored in the absorbent solution storage tank 11 and quantitatively fed into the slurry mixing tank 15 by the absorbent solution pump 12. Fly ash that has passed through a 200-mesh sieve (i.e., particle size ≤ 75 μm) is stored in the ash silo 13 and quantitatively fed into the slurry mixing tank 15 by the screw feeder 14. The liquid-ash ratio of the absorbent solution to the fly ash in the slurry mixing tank 15 is 1L:1kg. After thorough mixing for 1 hour, slurry is obtained. The slurry is pumped by the slurry pump 16 into the slurry hydrocyclone 17 for solid-liquid separation, yielding a clear liquid and a concentrated slurry. Part of the clear liquid is returned to the slurry mixing tank 15 for remixing, part of the clear liquid is stored in the clear liquid storage tank 19, and all of the concentrated slurry is stored in the concentrated slurry tank 18.

[0141] (2) CO2 absorption unit

[0142] After denitrification, dust removal, and desulfurization, the flue gas flows upward through the water washing tower 22. Cool water is pumped to the top of the water washing tower 22 by the cooling water pump 21 and sprayed downward through nozzles 22a, cooling the flue gas to about 40°C. Then, it is sent to the bottom of the absorption tower 26 by the induced draft fan 23 and flows upward. The clear liquid in the clear liquid storage tank 19 is pumped to the top of the absorption tower 26 by the clear liquid pump 24 and the clear liquid cooler 25. It is then atomized by nozzles 26a and sprayed out, capturing CO2 in the flue gas to obtain a carbon-rich absorbent liquid. The liquid-to-gas ratio of the clear liquid to the flue gas in the absorption tower 26 is 1L:1m³. 3 The gas velocity in the empty tower is 3 m / s.

[0143] To improve the utilization rate of the absorbent and the CO2 capture rate, the carbon-rich absorbent at the bottom of the absorber 26 is further returned to the top of the absorber 26 through the circulation pump 27 and the carbon-rich absorbent cooler 28, and then atomized and sprayed out through the nozzle 26a to capture CO2 in the flue gas again. The tail gas after the reaction is demisted and discharged from the top of the tower.

[0144] (3) Mineralization reaction unit

[0145] The carbon-rich absorbent liquid at the bottom of the absorber tower 26 is discharged periodically by the carbon-rich absorbent liquid pump 31, and after being heated by the heat exchanger 32, it is sent to the mineralization reactor 34. The concentrated slurry in the slurry tank 18 is sent to the mineralization reactor 34 by the concentrated slurry pump 33. The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry in the mineralization reactor 34 is 3:1. After the carbon-rich absorbent liquid and the concentrated slurry are mixed evenly, the temperature of the mineralization reactor 34 is raised to 220°C by steam heating, and the mineralization reaction is carried out at a pressure of 2.0 MPa to obtain a mineralized slurry. After the reaction is completed in 1 hour, heating is stopped, and cooling water is introduced to cool the mineralized slurry to below 100°C. Then, the mineralized slurry is discharged by the mineralized slurry pump 35 and sent to the mineralized slurry hydrocyclone 36 for solid-liquid separation to obtain mineralized ash and mineralized clear liquid. After being cooled by heat exchanger 32, the mineralized liquid is sent to liquid storage tank 19 for recycling. The mineralized ash residue is dehydrated by vacuum belt dewatering machine 37 and then utilized as a resource.

[0146] Example 2

[0147] Please refer to Table 1. The absorbent in this embodiment contains 22 wt.% Na2CO3, 4 wt.% MEA and 4 wt.% PZ, and the industrial solid waste is fly ash with a CaO content of 25%.

[0148] (1) Preprocessing unit

[0149] Please see Figure 1 The prepared absorbent solution is stored in the absorbent solution storage tank 11 and quantitatively fed into the slurry mixing tank 15 by the absorbent solution pump 12. Fly ash that has passed through a 200-mesh sieve (i.e., particle size ≤ 75μm) is stored in the ash silo 13 and quantitatively fed into the slurry mixing tank 15 by the screw feeder 14. The liquid-ash ratio of the absorbent solution to the fly ash in the slurry mixing tank 15 is 1L:1.1kg. After thorough mixing for 1 hour, slurry is obtained. The slurry is pumped by the slurry pump 16 into the slurry hydrocyclone 17 for solid-liquid separation, yielding a clear liquid and a concentrated slurry. Part of the clear liquid is returned to the slurry mixing tank 15 for remixing, part of the clear liquid is stored in the clear liquid storage tank 19, and all of the concentrated slurry is stored in the concentrated slurry tank 18.

[0150] (2) CO2 absorption unit

[0151] After denitrification, dust removal, and desulfurization, the flue gas flows upward through the water washing tower 22. Cool water is pumped to the top of the water washing tower 22 by the cooling water pump 21 and sprayed downward through nozzles 22a, cooling the flue gas to about 40°C. Then, it is sent to the bottom of the absorption tower 26 by the induced draft fan 23 and flows upward. The clear liquid in the clear liquid storage tank 19 is pumped to the top of the absorption tower 26 by the clear liquid pump 24 and the clear liquid cooler 25. It is then atomized by nozzles 26a and sprayed out, capturing CO2 in the flue gas to obtain a carbon-rich absorbent liquid. The liquid-to-gas ratio of the clear liquid to the flue gas in the absorption tower 26 is 1.2L:1m³. 3 The empty tower gas velocity of the flue gas is 2.5 m / s.

[0152] To improve the utilization rate of the absorbent and the CO2 capture rate, the carbon-rich absorbent at the bottom of the absorber 26 is further returned to the top of the absorber 26 through the circulation pump 27 and the carbon-rich absorbent cooler 28, and then atomized and sprayed out through the nozzle 26a to capture CO2 in the flue gas again. The tail gas after the reaction is demisted and discharged from the top of the tower.

[0153] (3) Mineralization reaction unit

[0154] The carbon-rich absorbent liquid at the bottom of the absorber tower 26 is discharged periodically by the carbon-rich absorbent liquid pump 31, and after being heated by the heat exchanger 32, it is sent to the mineralization reactor 34. The concentrated slurry in the slurry tank 18 is sent to the mineralization reactor 34 by the concentrated slurry pump 33. The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry in the mineralization reactor 34 is 3:1. After the carbon-rich absorbent liquid and the concentrated slurry are mixed evenly, the temperature of the mineralization reactor 34 is raised to 200°C by steam heating, and the mineralization reaction is carried out at a pressure of 1.5 MPa to obtain a mineralized slurry. After the reaction is carried out for 1.5 hours, heating is stopped, and cooling water is introduced to cool the mineralized slurry to below 100°C. Then, the mineralized slurry is discharged by the mineralized slurry pump 35 and sent to the mineralized slurry hydrocyclone 36 for solid-liquid separation to obtain mineralized ash and mineralized clear liquid. After being cooled by heat exchanger 32, the mineralized liquid is sent to liquid storage tank 19 for recycling. The mineralized ash residue is dehydrated by vacuum belt dewatering machine 37 and then utilized as a resource.

[0155] Example 3

[0156] Please refer to Table 1. The absorbent in this embodiment contains 25 wt.% Na2CO3, 2 wt.% MEA and 3 wt.% PZ; the industrial solid waste is fly ash with a CaO content of 25%.

[0157] (1) Preprocessing unit

[0158] Please see Figure 1 The prepared absorbent solution is stored in the absorbent solution storage tank 11 and quantitatively fed into the slurry mixing tank 15 by the absorbent solution pump 12. Fly ash that has passed through a 200-mesh sieve (i.e., particle size ≤ 75μm) is stored in the ash silo 13 and quantitatively fed into the slurry mixing tank 15 by the screw feeder 14. The liquid-ash ratio of the absorbent solution to the fly ash in the slurry mixing tank 15 is 1L:1.2kg. After thorough mixing for 1 hour, slurry is obtained. The slurry is pumped by the slurry pump 16 into the slurry hydrocyclone 17 for solid-liquid separation, yielding a clear liquid and a concentrated slurry. Part of the clear liquid is returned to the slurry mixing tank 15 for remixing, part of the clear liquid is stored in the clear liquid storage tank 19, and all of the concentrated slurry is stored in the concentrated slurry tank 18.

[0159] (2) CO2 absorption unit

[0160] After denitrification, dust removal, and desulfurization, the flue gas flows upward through the water washing tower 22. Cool water is pumped by the cooling water pump 21 to the upper part of the water washing tower 22 and sprayed downward through nozzles 22a, cooling the flue gas to about 40°C. Then, it is sent by the induced draft fan 23 to the bottom of the absorption tower 26 and flows upward. The clear liquid in the clear liquid storage tank 19 is pumped by the clear liquid pump 24 and the clear liquid cooler 25 to the top of the absorption tower 26, where it is atomized by nozzles 26a and sprayed out, capturing CO2 in the flue gas to obtain a carbon-rich absorbent liquid. The liquid-to-gas ratio of the clear liquid to the flue gas in the absorption tower 26 is 1.5L:1m³. 3 The gas velocity in the empty tower is 2 m / s.

[0161] To improve the utilization rate of the absorbent and the CO2 capture rate, the carbon-rich absorbent at the bottom of the absorber 26 is further returned to the top of the absorber 26 through the circulation pump 27 and the carbon-rich absorbent cooler 28, and then atomized and sprayed out through the nozzle 26a to capture CO2 in the flue gas again. The tail gas after the reaction is demisted and discharged from the top of the tower.

[0162] (3) Mineralization reaction unit

[0163] The carbon-rich absorbent liquid at the bottom of the absorber tower 26 is discharged periodically by the carbon-rich absorbent liquid pump 31, and after being heated by the heat exchanger 32, it is sent to the mineralization reactor 34. The concentrated slurry in the slurry tank 18 is sent to the mineralization reactor 34 by the concentrated slurry pump 33. The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry in the mineralization reactor 34 is 3:1. After the carbon-rich absorbent liquid and the concentrated slurry are mixed evenly, the temperature of the mineralization reactor 34 is raised to 180°C by steam heating, and the mineralization reaction is carried out at a pressure of 1.0 MPa to obtain a mineralized slurry. After the reaction is carried out for 2 hours, heating is stopped, and cooling water is introduced to cool the mineralized slurry to below 100°C. Then, the mineralized slurry is discharged by the mineralized slurry pump 35 and sent to the mineralized slurry hydrocyclone 36 for solid-liquid separation to obtain mineralized ash and mineralized clear liquid. After being cooled by heat exchanger 32, the mineralized liquid is sent to liquid storage tank 19 for recycling. The mineralized ash residue is dehydrated by vacuum belt dewatering machine 37 and then utilized as a resource.

[0164] Comparative Example 1

[0165] The mineralization method of this comparative example is basically the same as that of Example 1, except that the absorbent in this comparative example contains only 30 wt.% Na2CO3.

[0166] Comparative Example 2

[0167] The mineralization method of this comparative example is basically the same as that of Example 1, except that the absorbent in this comparative example contains 22 wt.% Na2CO3 and 8 wt.% MEA.

[0168] Comparative Example 3

[0169] The mineralization method of this comparative example is basically the same as that of Example 1, except that the absorbent in this comparative example contains 28 wt.% Na2CO3 and 2 wt.% PZ.

[0170] Comparative Example 4

[0171] The mineralization method of this comparative example is basically the same as that of Example 1, except that the absorbent in this comparative example contains 20 wt.% MEA and 10 wt.% PZ.

[0172] Comparative Example 5

[0173] The mineralization method in this comparative example is basically the same as that in Example 1, except that the temperature of the mineralization reaction is 120°C and the pressure is 0.8 MPa.

[0174] Comparative Example 6

[0175] The mineralization method in this comparative example is basically the same as that in Example 1, except that this comparative example does not have a pretreatment step, i.e., it does not mix the absorbent liquid and fly ash. The specific steps are as follows:

[0176] (1) CO2 absorption unit

[0177] Please see Figure 1 After denitrification, dust removal, and desulfurization, the flue gas flows upward through the water washing tower 22. Cool water is pumped to the top of the water washing tower 22 by the cooling water pump 21 and sprayed downward through nozzles 22a, cooling the flue gas to about 40°C. Then, it is sent to the bottom of the absorption tower 26 by the induced draft fan 23 and flows upward. The prepared absorbent (containing 20 wt.% Na2CO3, 8 wt.% MEA, and 2 wt.% PZ) is stored in the clear liquid storage tank 19 and sent to the top of the absorption tower 26 after passing through the clear liquid pump 24 and clear liquid cooler 25. It is then atomized by nozzles 26a and sprayed out to capture CO2 in the flue gas, resulting in a carbon-rich absorbent. The liquid-to-gas ratio of the absorbent to the flue gas in the absorption tower 26 is 1 L: 1 m³. 3 The gas velocity in the empty tower is 3 m / s.

[0178] To improve the utilization rate of the absorbent and the CO2 capture rate, the carbon-rich absorbent at the bottom of the absorber 26 is further returned to the top of the absorber through the circulation pump 27 and the carbon-rich absorbent cooler 28, and then atomized and sprayed out through the nozzle 26a to capture CO2 in the flue gas again. The tail gas after the reaction is demisted and discharged from the top of the tower.

[0179] (2) Mineralization reaction unit

[0180] The carbon-rich absorbent liquid at the bottom of the absorption tower 26 is discharged periodically by the carbon-rich absorbent liquid pump 31, and after being heated by the heat exchanger 32, it is sent to the mineralization reactor 34. Fly ash passing through a 200-mesh sieve (i.e., particle size ≤ 75 μm) is stored in the ash silo 13 and quantitatively fed into the mineralization reactor 34 by the screw feeder 14. The liquid-to-ash ratio of the carbon-rich absorbent liquid to the fly ash in the mineralization reactor 34 is 1 L: 1 kg. The mineralization reactor 34 is heated to 220°C by steam heating, and the mineralization reaction is carried out under a pressure of 2.0 MPa to obtain a mineralization slurry. After 1 hour of reaction, heating is stopped, and cooling water is introduced to cool the mineralization slurry to below 100°C. Then, the mineralization slurry is discharged by the mineralization slurry pump 35 and sent to the mineralization slurry hydrocyclone 36 for solid-liquid separation to obtain mineralized ash residue and mineralized clear liquid. After being cooled by heat exchanger 32, the mineralized liquid is sent to liquid storage tank 19 for recycling. The mineralized ash residue is dehydrated by vacuum belt dewatering machine 37 and then utilized as a resource.

[0181] The CO2 mineralization systems in Examples 1-3 and Comparative Examples 1-6 were all in continuous operation. Considering factors such as absorbent loss and the non-renewability of some absorbents, the CO2 capture rate, CO2 mineralization capacity, and fly ash mineralization efficiency were calculated using the following methods, and the results are shown in Table 1.

[0182] The CO2 concentration and flue gas flow rate before and after capture were measured using a comprehensive flue gas analyzer. The mass fractions of CaO, MgO, and SO3 in fly ash were determined using X-ray fluorescence spectroscopy (XRF), and the mass fraction of CaCO3 in fly ash was determined using chemical titration. These values ​​are expressed as m. CaO , m MgO The sampling target before capture refers to the flue gas before it enters the absorption tower, while the sampling target after capture refers to the exhaust gas discharged from the absorption tower; the unit of CO2 concentration is grams per standard cubic meter (g / Nm³). 3 The unit of flue gas flow rate is standard cubic meters per minute (Nm³). 3 / min), where N represents the standard conditions, namely, air conditions of 1 atm pressure, 0℃ temperature, and 0% relative humidity.

[0183] The formula for calculating the CO2 capture rate is: CO2 capture rate = [(CO2 concentration before capture × flue gas flow rate before capture - CO2 concentration after capture × flue gas flow rate after capture) / CO2 concentration before capture × flue gas flow rate before capture] × 100%.

[0184] The unit of CO2 mineralization capacity is grams of carbon dioxide per kilogram of fly ash (gCO2 / kg fly ash). The calculation formula is: CO2 mineralization capacity = CO2 capture amount per unit time / fly ash feed amount per unit time = (CO2 concentration before capture × flue gas flow rate before capture - CO2 concentration after capture × flue gas flow rate after capture) / fly ash feed amount per unit time.

[0185] The unit for the theoretical CO2 mineralization capacity of fly ash is also gCO2 / kg fly ash, and its calculation formula is:

[0186]

[0187] The formula for calculating the mineralization efficiency of fly ash is: Fly ash mineralization efficiency = (CO2 mineralization capacity / theoretical CO2 mineralization capacity of fly ash) × 100%.

[0188] Table 1. Relevant parameters and test data of the mineralization reaction in Examples 1-3 and Comparative Examples 1-6

[0189]

[0190] As shown in Table 1, in Examples 1-3, the absorbent was prepared by compounding Na2CO3, MEA, and PZ, with the total content of organic alkali not exceeding 10 wt.%, and the mineralization reaction was carried out at 180℃-220℃. Ultimately, a CO2 capture rate of 88.1%-90.3%, a CO2 mineralization capacity of 146.8 g / kg-180.6 g / kg, and a fly ash mineralization efficiency of 74.7%-88.5% were achieved. This indicates that the multi-component mixed absorbent in Examples 1-3 not only improves the CO2 capture rate and CO2 utilization rate, but also has the advantages of low organic alkali consumption, low absorbent regeneration energy consumption, and good economic efficiency.

[0191] In Comparative Example 1, the absorbent contained only 30 wt.% Na₂CO₃. Without the addition of organic alkali, its CO₂ capture rate was significantly reduced, resulting in a noticeably lower CO₂ mineralization capacity and fly ash mineralization efficiency. In Comparative Examples 2 and 3, the absorbent consisted of a combination of one organic alkali and another organic alkali; however, their CO₂ capture rate, CO₂ mineralization capacity, and fly ash mineralization efficiency were all lower than in Example 1, where the fly ash feed amount was the same. In Comparative Example 4, the absorbent consisted of a combination of two organic alkalis. Its CO₂ capture rate, CO₂ mineralization capacity, and fly ash mineralization efficiency were all lower than in Example 1, where the fly ash feed amount was the same. Moreover, the organic alkali feed amount in this CO₂ mineralization system was very large, resulting in very high energy consumption for absorbent regeneration. Furthermore, the organic alkali was prone to oxidative degradation at high temperatures and could not be regenerated, leading to poor economic efficiency for the entire CO₂ mineralization system.

[0192] The absorbent in Comparative Example 5 was the same as that in Example 1. However, due to the lower reaction temperature and slower reaction rate of the mineralization reaction, the consumption of absorbent was larger and the regeneration rate was slower. As a result, the CO2 capture rate, CO2 mineralization capacity and fly ash mineralization efficiency of the entire system under continuous operation were significantly reduced.

[0193] In Comparative Example 6, the absorbent and fly ash were not mixed before CO2 absorption and mineralization, which resulted in a significant decrease in the absorbent's ability to absorb CO2 and a reduction in the reaction rate of the mineralization reaction. Therefore, the CO2 capture rate, CO2 mineralization capacity, and fly ash mineralization efficiency of this system were not ideal.

[0194] Understandably, with the same amount of fly ash fed, the CO2 capture rate, CO2 mineralization capacity, and fly ash mineralization efficiency of Example 1 are significantly better than any of the comparative examples. Furthermore, the CO2 mineralization capacity and fly ash mineralization efficiency of Example 3 are only slightly higher than those of Comparative Example 2, and lower than those of Comparative Examples 4 and 6. This is because the amount of fly ash fed in Example 3 is relatively high, leading to a decrease in the calculated CO2 mineralization capacity and fly ash mineralization efficiency of Example 3.

[0195] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0196] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the invention patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these all fall within the protection scope of the present invention. Therefore, the protection scope of this invention patent should be determined by the appended claims, and the specification and drawings can be used to interpret the content of the claims.

Claims

1. A method for carbon dioxide mineralization, characterized in that, Includes the following steps: The absorbent liquid and industrial solid waste are mixed at room temperature, wherein the room temperature range is 20℃~30℃, to obtain mortar. The mortar is separated into solid and liquid components to obtain a clear liquid and a concentrated mortar. The clear liquid is used to absorb carbon dioxide from the flue gas to obtain a carbon-rich absorbent liquid. The carbon-rich absorbent liquid and the concentrated slurry are subjected to a mineralization reaction at 180℃~220℃ to obtain a mineralized slurry. The mineralized slurry is subjected to solid-liquid separation to obtain mineralized ash and mineralized clear liquid; The absorbent liquid comprises an inorganic base and an organic base, wherein the organic base comprises at least two of monoethanolamine, diethanolamine, triethanolamine, 3-methylaminopropylamine, N-methyldiethanolamine, piperazine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, and 2-amino-2-methyl-1-propanolamine.

2. The method for carbon dioxide mineralization as described in claim 1, characterized in that, The organic base is monoethanolamine and piperazine.

3. The method for carbon dioxide mineralization as described in claim 2, characterized in that, The organic base in the absorbent has a content of 4 wt.% to 12 wt.%.

4. The method for carbon dioxide mineralization as described in claim 3, characterized in that, The organic base satisfies one or more of the following conditions: 1) The content of the monoethanolamine in the absorbent is 2 wt.%~8 wt.%; 2) The content of the piperazine in the absorbent is 2 wt.% to 4 wt.%.

5. The method for carbon dioxide mineralization as described in any one of claims 1 to 4, characterized in that, The inorganic base satisfies one or more of the following conditions: 1) The content of the inorganic base in the absorbent is 20 wt.%~25 wt.%; 2) The inorganic base includes one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, potassium carbonate and sodium phosphate.

6. The method for carbon dioxide mineralization as described in claim 5, characterized in that, The step of mixing the absorbent and the industrial solid waste satisfies one or more of the following conditions: 1) The liquid-to-solid ratio of the absorbent to the industrial solid waste is 1L:(1kg~1.2kg). 2) The mixing time of the absorbent and the industrial solid waste is 0.5h to 1h.

7. The method for carbon dioxide mineralization as described in claim 5, characterized in that, The step of allowing the clarified liquid to absorb carbon dioxide from the flue gas satisfies one or more of the following conditions: 1) The gas velocity of the flue gas is 2m / s to 3m / s; 2) The temperature of the flue gas is 35℃~45℃; 3) The carbon dioxide concentration in the flue gas is 200 g / Nm³. 3 ~300g / Nm 3 ; 4) The liquid-to-gas ratio of the clarified liquid to the flue gas is (1L~1.5L):1m 3 .

8. The method for carbon dioxide mineralization as described in claim 5, characterized in that, The mineralization reaction satisfies one or more of the following conditions: 1) The reaction pressure of the mineralization reaction is 1.0 MPa to 2.0 MPa; 2) The reaction time for the mineralization reaction is 1 to 2 hours; 3) The volume ratio of the carbon-rich absorbent liquid to the concentrated slurry is (2~3):

1.

9. The method for carbon dioxide mineralization as described in any one of claims 1 to 4, characterized in that, The industrial solid waste meets one or more of the following conditions: 1) The calcium oxide content of the industrial solid waste is ≥10 wt.%; 2) The particle size of the industrial solid waste is ≤75μm; 3) The industrial solid waste includes one or more of the following: fly ash, steel slag, carbide slag, waste cement, and waste gypsum.

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