Method for intensively mineralizing carbon dioxide in air

Abstract

The invention relates to the technical field of CO2 trapping, in particular to a method for intensively mineralizing carbon dioxide in air, which comprises the following steps: uniformly mixing a mineralization absorbent and an absorption auxiliary material, putting the mixture into a tray reactor, enabling air to penetrate through a mixed material bed layer in the tray reactor from top to bottom or from bottom to top, and separating the mixed material by using a screen after mineralization is completed, recycling an absorption auxiliary material, and carrying out landfill treatment on a mineralized absorbent; wherein the mineralization absorbent comprises any one or a mixture of more of alkaline industrial waste and calcium hydroxide; the absorption auxiliary material comprises any one or more of West ring, Pall ring, Raschig ring, wood shavings, straw, bran, coco coir, sawdust, cloth strips and cotton yarns. The addition of the absorption auxiliary material not only improves the void ratio in the mineralization absorbent bed layer, reduces the bed layer resistance and enhances the gas distribution uniformity, but also obviously improves the gas-solid contact outer area of the mineralization absorbent and air. Therefore, the method greatly improves the absorption efficiency of direct mineralization of carbon dioxide.

Description

Technical Field

[0001] The invention relates to the technical field of capturing CO2, and in particular to a method for enhancing the mineralization of carbon dioxide in air. Background Art

[0002] With the acceleration of global industrialization, the concentration of carbon dioxide (CO2) in the earth's atmosphere has continued to rise and has reached a record high, and the global warming problem caused by this has become increasingly serious. In this context, Direct Air Capture (DAC) technology has received extensive attention and research as one of the means to effectively remove carbon dioxide from the atmosphere. However, compared with point source capture where emission sources are more concentrated, the concentration of CO2 in the atmosphere is relatively low, which puts higher requirements on the efficiency and cost of DAC technology.

[0003] At present, a variety of capture methods have been developed in the field of DAC technology, among which the inorganic base circulation method, solid alkali (earth) metal circulation method and solid amine temperature-swing adsorption and desorption method are relatively mature and have been industrialized. In particular, the calcium circulation process, as an important branch of the solid alkali (earth) metal circulation method, has become a research hotspot in the DAC field with its low raw material cost and good environmental adaptability.

[0004] However, the existing DAC technology still faces many challenges in increasing the contact area between the absorbent and the air and improving the capture efficiency. Taking the calcium hydroxide single-cycle method as an example, although a larger contact area can be formed by dispersing calcium hydroxide in a flat manner in the tray, this method requires a large number of trays, which increases the workload of loading and unloading, and is not conducive to large-scale application. To solve this problem, researchers have tried to use a fluidized bed process to increase the contact area between the absorbent and the air through fluidization, but this is accompanied by problems such as difficulty in recovering the absorbent, high energy consumption, and high investment costs. Although the fixed bed process is easy to operate, when dealing with low-concentration CO2 (such as 410ppm in the atmosphere), there are limitations such as uneven airflow distribution, large pressure drop, strict requirements on the shape of the absorbent, and long mineralization cycle, resulting in limited equipment production capacity and difficulty in meeting the needs of large-scale carbon capture.

[0005] In view of the above technical bottlenecks, improving the absorption rate per unit area has become the key to improving the performance of DAC technology. Specifically, it includes improving the air permeability of the absorbent and increasing the contact area between the absorbent and the air. However, due to factors such as the large air permeability resistance of the absorbent and the limited diffusion radius, the existing technology still faces great difficulties in improving the absorption rate.

[0006] In view of this, the present invention is proposed. Summary of the invention

[0007] The object of the present invention is to provide a method for enhancing the mineralization of carbon dioxide in air, which significantly increases the gas-solid contact external area between the mineralization absorbent and air, thereby improving the absorption efficiency of direct carbon dioxide mineralization.

[0008] The present invention provides a method for enhancing the mineralization of carbon dioxide in air, comprising the following steps:

[0009] Mix the mineralization absorbent with the absorption auxiliary materials and then load them into a tray reactor. Air passes through the mixed material bed layer in the tray reactor from top to bottom or from bottom to top. The mixed materials mineralize and absorb the carbon dioxide in the air. After mineralization is completed, the mixed materials are separated using a sieve, the absorption auxiliary materials are recycled, and the mineralization absorbent is landfilled;

[0010] Wherein, the mineralization absorbent is a mixture of any one or more of calcium hydroxide and alkaline industrial waste;

[0011] The absorption auxiliary materials include any one or more of saddles, pall rings, raschig rings, wood shavings, straw, bran, coir pith, wood chips, cloth strips, and cotton yarn.

[0012] The present invention mixes the mineralization absorbent with fillers such as saddles, pall rings, raschig rings, and organic matter absorption auxiliary materials such as wood shavings, straw, bran, and coir pith, which not only increases the porosity of the bed layer, reduces the resistance when the air flow passes through, but also promotes the uniform distribution of gas, ensuring that the carbon dioxide in the air can more effectively contact the mineralization absorbent and improving the overall reaction efficiency. At the same time, the addition of the absorption auxiliary materials, especially those organic or inorganic fillers with a large specific surface area, significantly increases the contact area between the mineralization absorbent and air, thereby increasing the treatment amount of carbon dioxide per unit time.

[0013] Preferably in this technical solution, during the mineralization absorption process, every 2 - 72 h, the mixed materials are transferred to a mixer, thoroughly turned and mixed evenly, and then reloaded into the tray reactor.

[0014] Regularly turning and mixing the mixed materials can ensure sufficient contact between the mineralization absorbent and the carbon dioxide in the air, avoiding local saturation or underutilization. Moreover, long-term operation may cause blockage or compaction of the material bed layer, and turning and mixing can effectively alleviate this problem and maintain the permeability of the material bed layer; in addition, through regular turning and mixing, local wear of the materials in the tray reactor can be reduced, thereby extending the overall service life and ensuring uniform consumption of the mineralization absorbent throughout the bed layer, avoiding a decline in the overall performance caused by local excessive consumption; finally, the turning and mixing operation can adjust the reaction rate during the mineralization absorption process to make it more stable and controllable. For carbon dioxide air with different concentrations, the mineralization absorption effect can be further optimized by adjusting the turning and mixing frequency and time.

[0015] Preferably, in the technical solution, the mass ratio of the mineralized absorbent to the absorption auxiliary material of the present invention is 1:(0.02 - 2), and preferably 1:(0.08 - 0.5).

[0016] When the mass ratio of the mineralized absorbent to the absorption auxiliary material is within this range, the mineralized absorbent and the absorption auxiliary material can form an effective mixing system to ensure that carbon dioxide in the air is fully absorbed. Moreover, absorption auxiliary materials such as theta rings and Pall rings have a porous structure, which is conducive to the mass transfer process of gas and liquid, increases the permeability of the mixed material bed layer, enables air to penetrate more easily and come into full contact with the mineralized absorbent, and further improves the mineralization absorption effect. In addition, the mixing of the mineralized absorbent and the absorption auxiliary material can prevent the agglomeration of the mineralized absorbent particles and maintain their dispersed state, thereby prolonging the service life of the mineralized absorbent and reducing the performance degradation caused by agglomeration. Furthermore, the addition of the absorption auxiliary material can increase the mechanical strength of the mixed material, making it more capable of withstanding the pressure and friction in the tray reactor, maintaining the stability of the material bed layer in the reactor, and ensuring the smooth progress of the mineralization absorption process.

[0017] Preferably, in the technical solution, the particle size of the mineralized absorbent is 40 - 200 mesh, preferably 60 - 150 mesh; the particle size of the absorption auxiliary material is 0.2 - 10 cm.

[0018] When the mineralized absorbent and the absorption auxiliary material are within the above particle size ranges, firstly, the particles of the mineralized absorbent are fine and have a large specific surface area, which can come into full contact with carbon dioxide in the air, help the gas diffuse into the interior of the particles, increase the reaction interface, and thus improve the mineralization absorption efficiency. The relatively larger particle size of the absorption auxiliary material can form a porous structure, providing more reaction channels for the mineralization reaction, making it easier for the gas to penetrate the mixed material bed layer and facilitating the passage of the gas and the absorption of carbon dioxide. Secondly, the difference in particle size between the mineralized absorbent and the absorption auxiliary material enables them to form a more uniform distribution during mixing, avoiding local accumulation or agglomeration phenomena, and helping to form more voids during the mixing process, improving the fluidity of the material and making the mixing more uniform. Thirdly, the fine particles of the mineralized absorbent are not easily blocked at the outlet or sieve of the tray reactor, which can effectively ensure the smooth progress of the mineralization absorption process, while the particle structure of the absorption auxiliary material can form a certain supporting effect to prevent the material from being compacted or blocked in the reactor.

[0019] Preferably, in the technical solution, the alkaline industrial waste includes any one or more of carbide slag, steel slag, and fly ash.

[0020] Among them, carbide slag, as a by-product in the production of calcium carbide, is rich in calcium hydroxide and has strong alkalinity, which can effectively absorb carbon dioxide.

[0021] Steel slag is a by-product in the steel production process, rich in various minerals, including silicates, etc., and these components can play an important role in the mineralization process.

[0022] Fly ash is a waste from coal-fired power plants, rich in elements such as silicon and aluminum, and can be used to prepare mineralization absorbents.

[0023] Preferably in this technical solution, a plurality of through holes are evenly opened at the bottom of the tray reactor, the diameter of the through holes is 20-100 mesh, and specifically, breathable materials such as perforated plates, sieves, non-woven fabrics, and multi-layer sintered meshes can be used.

[0024] Preferably in this technical solution, a reinforcing structure is detachably arranged below the tray reactor to carry enough mineralization absorbents and auxiliary materials.

[0025] Preferably in this technical solution, the temperature of the air is 4-40 °C and the absolute humidity is 3-30 g / kg. The method of the present invention is applicable to various environmental conditions, including indoor, outdoor, warm or cold regions, etc., and the types and proportions of mineralization absorbents and absorption auxiliary materials can be adjusted according to actual needs to adapt to different carbon dioxide concentrations and treatment requirements.

[0026] Preferably in this technical solution, the speed of the air passing through the tray reactor is 0.05-2 m / s. By controlling the speed of the air passing through the tray reactor, the efficiency and rate of carbon dioxide mineralization can be controlled.

[0027] Preferably in this technical solution, the moisture content of the mixed material is 1 wt%-10 wt%.

[0028] Controlling the moisture content of the mixed material within the range of 1 wt%-10 wt% helps to maintain the appropriate humidity of the material, keep the mineralization absorbent active, and then promote the chemical reaction between the mineralization absorbent and carbon dioxide, accelerate the formation of mineralization products, and at the same time avoid blockage or decreased absorption efficiency caused by excessive moisture.

[0029] The method for strengthening the mineralization of carbon dioxide in the air of the present invention has at least the following beneficial effects:

[0030] In the method for strengthening the mineralization of carbon dioxide in air according to the present invention, calcium hydroxide or alkaline industrial waste is used as the mineralization absorbent. Due to their alkaline mineral components, these materials have the ability to rapidly carry out chemical reactions with low-concentration carbon dioxide, thereby effectively converting carbon dioxide in air into stable carbonates. More importantly, in the present invention, the mineralization absorbent is mixed with fillers such as saddles, pall rings, raschig rings, as well as organic matter absorption auxiliary materials such as wood shavings, straw, wheat bran, coconut coir, and sawdust. This not only increases the porosity of the bed layer, reduces the resistance when the air flow passes through, but also promotes the uniform distribution of the gas, ensuring that the carbon dioxide in the air can more effectively contact the mineralization absorbent and improving the overall reaction efficiency. At the same time, the addition of the absorption auxiliary materials, especially those organic or inorganic fillers with a large specific surface area, significantly increases the contact area between the mineralization absorbent and the air, thereby increasing the processing amount of carbon dioxide per unit time. Finally, the absorption auxiliary materials in the present invention can be easily separated through a sieve after the mineralization process is completed and reused, which not only reduces the operating cost but also promotes the recycling of resources, meeting the concepts of green chemistry and sustainable development.

[0031] Therefore, the method for strengthening the mineralization of carbon dioxide in air according to the present invention significantly improves the direct mineralization absorption efficiency of carbon dioxide by optimizing the bed layer structure and enhancing the gas-solid contact area, and is more suitable for industrial scale-up. Detailed implementation manners

[0032] It should be noted that the following detailed descriptions are all illustrative and are intended to provide further explanations for the present application. Unless otherwise specified, all technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the technical field to which the present application belongs.

[0033] It should be noted that the terms used herein are only for describing specific implementation manners and are not intended to limit the exemplary implementation manners according to the present application. As used herein, unless the context clearly indicates otherwise, the singular form also includes the plural form. In addition, it should be understood that when the terms "comprise" and / or "include" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0034] The technical solutions of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are some, but not all, of the embodiments of the present invention. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0035] The carbide slag used in the following examples and comparative examples is a commercially available product, with a calcium hydroxide content of 80.43 wt% and a water content of 1.8 wt%; the steel slag is a commercially available product, with a total calcium content (calculated as CaO) of 38.11 wt% and a water content of 1.1%.

[0036] The tray reactor used in the following examples and comparative examples is a circular tray with a diameter of 1 m and a height of 10 cm. The bottom of the tray reactor is a 40-mesh metal screen and is supported by reinforcing ribs. A fan with the same diameter is placed below the tray reactor.

[0037] During the mineralization absorption process, the absolute humidity of the air is controlled to be 9 - 12 g / kg (dry air), the air temperature is 19 - 28 °C, and the volume concentration of CO2 in the air is 400 - 420 ppm by a humidifier; the wind speed is controlled by a fan and measured by an anemometer.

[0038] The carbonate in the raw materials and mineralization products of the present invention is determined by measuring the gas volume generated in the test sample by the hydrochloric acid method.

[0039] The calculation formula for the conversion rate C% of calcium hydroxide in the carbide slag sample is as follows:

[0040] C 氢氧化钙 % = 74 * (C2 - C 电石渣1 ) / C 电石渣0 (100 - 26C2)

[0041] Where: C 电石渣1 is the mass fraction of dry - basis calcium carbonate in the carbide slag, wt%;

[0042] C2 is the mass fraction of dry - basis calcium carbonate in the mineralization product, wt%;

[0043] C 电石渣0 is the mass fraction of dry - basis calcium hydroxide in the carbide slag, wt.

[0044] The absorption rate υ (g / m 2 / h) of CO2 per unit bed - area per unit time is calculated as follows:

[0045] υ = 44 * W1 * C0 * C% / (74 * S * t)

[0046] Where: W1 is the mass of dry - basis of the initial raw material, g;

[0047] C 电石渣0 is the mass fraction of dry - basis calcium hydroxide in the carbide slag, wt%;

[0048] C 氢氧化钙 % is the conversion rate of calcium hydroxide, % S is the bed - area, m 2 ;

[0049] t is the reaction time, h.

[0050] The calculation formula for the total calcium conversion rate C% in the steel slag sample is as follows:

[0051] C 总钙 % = 56 * (C2 - C 钢渣1 ) / C 钢渣0 (100 - 44C2)

[0052] Where: C 钢渣1 is the mass fraction of calcium carbonate on dry basis in the steel slag, wt%;

[0053] C2 is the mass fraction of calcium carbonate on dry basis in the mineralized product, wt%;

[0054] C 钢渣0 is the mass fraction of total calcium (calculated as calcium oxide) in the steel slag, wt.

[0055] The CO2 absorption rate υ (g / m 2 / h) per unit bed area per unit time is calculated as follows:

[0056] υ = 44 * W1 * C0 * C% / (56 * S * t)

[0057] Where: W1 is the mass of the initial raw material on dry basis, g;

[0058] C 钢渣0 is the mass fraction of total calcium (calculated as calcium oxide) in the steel slag, wt%;

[0059] C 总钙 % is the molar conversion rate of total calcium, % S is the bed area, m 2 ;

[0060] t is the reaction time, h.

[0061] Example 1

[0062] 8.3 kg of carbide slag and 6.6 kg of Raschig rings were mixed evenly and loaded into a tray reactor. Among them, the size of the carbide slag was 60 - 150 mesh, and the size of the Raschig rings was Φ6 mm * 6 mm.

[0063] Air was passed through the bed at an average wind speed of 0.1 m / s by a fan. When the mineralization reaction time reached 48 hours, the carbide slag and Raschig rings were remixed evenly and then reloaded into the tray reactor.

[0064] After 96 hours of absorption, the conversion rate of the carbide slag (calculated as the conversion rate of calcium hydroxide in the carbide slag) was 76.5%, and the CO2 absorption rate per unit area was 40.24 g / m 2 / h.

[0065] Finally, the mineralized mixed materials are separated using a sieve, the absorbed auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0066] Example 2

[0067] 10.7 kg of carbide slag and 8.1 kg of Sita rings are evenly mixed and loaded into a tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the Sita rings is Φ6 mm * 6 mm.

[0068] Air is passed through the bed by a fan at an average wind speed of 0.1 m / s. When the mineralization reaction time reaches the 48th hour and the 96th hour respectively, the carbide slag and the Sita rings are remixed evenly and then reloaded into the tray reactor.

[0069] After 115 hours of absorption, the conversion rate of the carbide slag (calculated based on the conversion rate of calcium hydroxide in the carbide slag) is 75.2%, and the CO2 absorption rate per unit area is 42.57 g / m 2 / h.

[0070] Finally, the mineralized mixed materials are separated using a sieve, the absorbed auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0071] Example 3

[0072] 12.1 kg of carbide slag and 9.7 kg of Sita rings are evenly mixed and loaded into a tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the Sita rings is Φ6 mm * 6 mm.

[0073] Air is passed through the bed by a fan at an average wind speed of 0.1 m / s. When the mineralization reaction time reaches the 48th hour and the 96th hour, the carbide slag and the Sita rings are remixed evenly and then reloaded into the tray reactor.

[0074] After 122 hours of absorption, the conversion rate of the carbide slag (calculated based on the conversion rate of calcium hydroxide in the carbide slag) is 73.4%, and the CO2 absorption rate per unit area is 44.3 g / m 2 / h.

[0075] Finally, the mineralized mixed materials are separated using a sieve, the absorbed auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0076] Example 4

[0077] 8.3 kg of carbide slag and 1.7 kg of wood shavings are evenly mixed and loaded into a tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the wood shavings is 5 - 7 mm.

[0078] Air is passed through the bed layer at an average wind speed of 0.1 m / s by a fan. After the mineralization reaction time reaches 48 hours, the carbide slag and wood shavings are remix and evenly mixed, and then reloaded into the tray reactor.

[0079] After 96 hours of absorption, the conversion rate of carbide slag (calculated based on the conversion rate of calcium hydroxide in carbide slag) is 71.2%, and the CO2 absorption rate per unit area is 37.45 g / m 2 / h.

[0080] Finally, the mineralized mixed material is separated using a sieve, the absorption auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0081] Example 5

[0082] 8.3 kg of carbide slag and 8 kg of Pall rings are evenly mixed and loaded into the tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the Pall rings is Φ8 mm * 8 mm.

[0083] Air is passed through the bed layer at an average wind speed of 0.1 m / s by a fan. After the mineralization reaction time reaches 48 hours, the carbide slag and Pall rings are remix and evenly mixed, and then reloaded into the tray reactor.

[0084] After 96 hours of absorption, the conversion rate of carbide slag (calculated based on the conversion rate of calcium hydroxide in carbide slag) is 73.8%, and the CO2 absorption rate per unit area is 38.82 g / m 2 / h.

[0085] Finally, the mineralized mixed material is separated using a sieve, the absorption auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0086] Example 6

[0087] 10.7 kg of carbide slag and 8.5 kg of theta rings are evenly mixed and loaded into the tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the theta rings is Φ8 mm * 8 mm.

[0088] Air is passed through the bed layer at an average wind speed of 0.1 m / s by a fan. When the mineralization reaction time reaches 48 hours and 96 hours, the carbide slag and theta rings are remix and evenly mixed, and then reloaded into the tray reactor.

[0089] After 110 hours of absorption, the conversion rate of carbide slag (calculated based on the conversion rate of calcium hydroxide in carbide slag) is 74.0%, and the CO2 absorption rate per unit area is 43.79 g / m 2 / h.

[0090] Finally, the mineralized mixed materials are separated using a sieve, the absorbed auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0091] Example 7

[0092] 17 kg of steel slag and 8 kg of theta rings are mixed evenly and loaded into a tray reactor. Among them, the size of the steel slag is 100 - 200 mesh, and the size of the theta rings is Φ8 mm * 8 mm.

[0093] Air is passed through the bed at an average wind speed of 0.05 m / s by a fan. When the mineralization reaction time reaches the 18th hour, the steel slag and theta rings are remix mixed evenly and then reloaded into the tray reactor.

[0094] After 33 hours of absorption, the conversion rate of the steel slag (calculated as the molar conversion rate of total calcium in the steel slag to calcium carbonate) is 18.3%, and the CO2 absorption rate per unit area is 35.56 g / m 2 / h.

[0095] Finally, the mineralized mixed materials are separated using a sieve, the absorbed auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0096] Control Example 1

[0097] 10.7 kg of carbide slag is placed in a tray reactor with a diameter of 1 m, and air is blown from the bottom up using the same fan and the same power as in Example 1. At the same time, an additional fan is used to blow air from the side across the tray reactor.

[0098] The carbide slag is remix mixed every 24 hours to expose the active surface on the outer surface.

[0099] After 220 hours of absorption, the conversion rate of the carbide slag (calculated as the conversion rate of calcium hydroxide in the carbide slag) is 65.2%, and the CO2 absorption rate per unit area is 23.48 g / m 2 / h.

[0100] Control Example 2

[0101] 8.3 kg of carbide slag and 6.6 kg of broken porcelain pieces are mixed evenly and loaded into a tray reactor. Among them, the size of the carbide slag is 60 - 150 mesh, and the size of the broken porcelain pieces is 0.5 - 1 cm.

[0102] Air is blown from the bottom up through the reactor using the same fan and the same power as in Example 1. When the mineralization reaction time reaches 24 hours each time, the carbide slag and broken porcelain pieces are remix mixed evenly and then reloaded into the tray reactor.

[0103] After 96 hours of absorption, the conversion rate of carbide slag (calculated based on the conversion rate of calcium hydroxide in carbide slag) is 49.1%, and the CO2 absorption rate per unit area is 25.78 g / m 2 / h.

[0104] Finally, the mineralized mixed materials are separated using a sieve, the absorption auxiliary materials are recycled, and the mineralized absorbent is sent to a designated location for landfill treatment to achieve permanent carbon sequestration.

[0105] Table 1 shows the mineralization absorption effects of Examples 1-7 and Comparative Examples 1-2

[0106]

[0107]

[0108] As can be seen from Table 1, in the method for enhancing the mineralization of carbon dioxide in Examples 1-7 of the present invention, after 70-180 hours of absorption, the conversion rate of the mineralizable components in the mineralized absorbent can reach 70%-80% (the conversion rate of steel slag is calculated separately due to component differences), and the CO2 absorption rate can reach 35-50 g / m 2 / h, which has excellent mineralization absorption effects compared with Comparative Examples 1-2.

[0109] In summary, the method for enhancing the mineralization of carbon dioxide in the air of the present invention significantly improves the direct mineralization absorption efficiency of carbon dioxide by optimizing the bed structure and enhancing the gas-solid contact area, and is more suitable for industrial scale-up.

[0110] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for enhancing the mineralization of carbon dioxide in air, characterized in that, It includes the following steps: Mix the mineralized absorbent with the absorption auxiliary materials and load them into the tray reactor. Air passes through the mixed material bed layer in the tray reactor from top to bottom or from bottom to top. The mixed materials carry out mineralization absorption on carbon dioxide in the air. After mineralization is completed, the mixed materials are separated using a sieve, the absorption auxiliary materials are recycled, and the mineralized absorbent is landfilled; Among them, the mineralized absorbent includes any one or a mixture of more than one of calcium hydroxide and alkaline industrial waste; The absorption auxiliary materials include any one or more of theta rings, Pall rings, Raschig rings, wood shavings, straw, wheat bran, coconut coir, wood chips, cloth strips, and cotton yarn.

2. The method for strengthening the mineralization of carbon dioxide in air according to claim 1, wherein During the mineralization absorption process, every 2 - 72 hours, transfer the mixed materials to a mixer, mix them thoroughly, and then reload them into the tray reactor.

3. The method for enhancing the mineralization of carbon dioxide in air according to claim 1, wherein The mass ratio of the mineralized absorbent to the absorption auxiliary materials is 1:(0.02 - 2).

4. The method for strengthening the mineralization of carbon dioxide in air according to claim 1, wherein The size of the mineralized absorbent is 0.01 - 2 mm, and the size of the absorption auxiliary materials is 0.2 - 10 cm.

5. The method for enhancing the mineralization of carbon dioxide in air according to claim 1, characterized in that, The alkaline industrial waste includes any one or more of carbide slag, steel slag, and fly ash.

6. The method for strengthening the mineralization of carbon dioxide in air according to claim 1, characterized in that, A plurality of through holes are evenly opened at the bottom of the tray reactor, and the diameter of the through holes is 20 - 100 mesh.

7. The method for strengthening the mineralization of carbon dioxide in air according to claim 1, wherein A strengthening structure is detachably arranged below the tray reactor.

8. The method for enhancing the mineralization of carbon dioxide in air according to claim 1, wherein, The temperature of the air is 4 - 40 °C, and the absolute humidity is 3 - 30 g / kg.

9. The method for enhancing the mineralization of carbon dioxide in air according to claim 1, wherein The speed of the air passing through the tray reactor is 0.05 - 2 m / s.

10. The method for enhancing the mineralization of carbon dioxide in air according to claim 1, wherein, The moisture content of the mixed materials is 1 wt% - 10 wt%.

Images