Mineral carbonation system linked with desulfurization process

Abstract

According to an embodiment of the present invention, a mineral carbonation system may comprise: a cooler which cools flue gas; a carbon dioxide absorption tower which absorbs carbon dioxide contained in the flue gas; a carbonation reactor which mixes a solution discharged from the carbon dioxide absorption tower and steel slag to carbonate a calcium-containing material in the steel slag; and a dehydrator which dehydrates the slag mixture obtained from the carbonation reactor to obtain carbonated slag.

Description

Mineral carbonation system linked with desulfurization process

[0001] The present invention relates to a mineral carbonation system linked with a desulfurization process.

[0002] The steelmaking process refers to the process of producing steel products by making molten iron using iron ore and coke as raw materials, followed by processes such as steelmaking and rolling. A typical steelmaking process involves feeding sintered iron ore and coke, produced by the carbonization of coal, into a blast furnace to produce molten iron.

[0003] Molten iron is produced through this process, and subsequently, a steelmaking process utilizing limestone is employed to adjust the composition of the molten iron. During this process, slag (steelmaking slag) containing a large amount of calcium is generated. Due to its high calcium content, steelmaking slag is widely used as a raw material for mineral carbonation, a component of CCUS (Carbon Capture Utilization & Storage) technology for the stable storage and utilization of CO2. Among mineral carbonation technologies, direct carbonation involves directly injecting flue gas containing carbon dioxide into a slurry (a mixture of industrial byproducts and water). This process causes the carbon dioxide to react with the alkali / alkaline earth metal components contained in the byproducts to form carbonates. However, since carbon dioxide dissolves in water and subsequently reacts with the industrial byproducts, it is difficult to control the amount of dissolved carbon dioxide and the reaction rate with the byproducts. Consequently, to ensure stable mineral carbonation and CO2 removal rates, this method has the disadvantage of requiring a larger reactor size due to the slow dissolution rate of CO2. In addition, water (liquid), industrial byproducts (solid), carbon dioxide, and inert gas (N2) must be handled within the reactor, and there may be a disadvantage that the energy required for mechanical devices to ensure the flow of these materials or for blowing exhaust gas is high.

[0004] Accordingly, technologies have been proposed to improve the quality and speed of slag mineral carbonation by utilizing an alkaline solution to pre-dissolve carbon dioxide, thereby securing a solution with an excess amount of dissolved carbon dioxide, and reacting it with slag. However, in slag mineral carbonation technology utilizing a solution capable of dissolving carbon dioxide, an additional washing process is required for the carbonated slag due to the water content (moisture) contained in the carbonated slag during the dehydration process of the mineral carbonation product. During washing, a low-concentration alkaline solution is generated, and if this is recycled for the carbon dioxide dissolution process, the problem of the total concentration of the alkaline solution for carbon dioxide dissolution continuously decreases, making it difficult to use the solution for carbon dioxide dissolution. Consequently, wastewater treatment of the solution is required, and since the solution requiring treatment is high-pH wastewater, there is a problem of having to appropriately adjust (neutralize) the pH before discharge.

[0005] Furthermore, CCUS technology involves a process for capturing CO2 from gases containing CO2 (CO2 capture). Since fuels often contain sulfur, these sulfur components transform into sulfur oxides (SOx) after combustion; therefore, compounds such as CaO, Ca(OH)2, CaCO3, and NaHCO3 are used to remove these sulfur oxides from the flue gas. If sulfur oxides are not removed from the flue gas, they can damage the absorbents in the CO2 capture process or, if released into the atmosphere, cause problems such as the generation of acid rain.

[0006] One embodiment of the present invention can provide a mineral carbonation system capable of stably fixing carbon dioxide and increasing the amount of fixation.

[0007] One embodiment of the present invention can provide a mineral carbonation system capable of improving the reaction rate of mineral carbonation.

[0008] One embodiment of the present invention can provide a mineral carbonation system capable of removing sulfur components from flue gas without additional chemicals.

[0009] One embodiment of the present invention can provide a mineral carbonation system capable of processing high pH slag dewatering liquid without a separate neutralization process.

[0010] The problems of the present invention are not limited to those described above. A person skilled in the art to which the present invention pertains will have no difficulty understanding additional problems of the present invention from the overall contents of this specification.

[0011] A mineral carbonation system, which is an embodiment of the present invention, includes: a cooler for cooling flue gas; a carbon dioxide absorption tower for absorbing carbon dioxide contained in flue gas; a carbonation reactor for mixing a solution discharged from the carbon dioxide absorption tower with ironmaking slag to carbonate calcium-containing substances in the ironmaking slag; and a dehydrator for dehydrating the slag mixture obtained from the carbonation reactor to obtain carbonated slag.

[0012] It may include a first pipe that supplies cooling water to the top of the above cooler.

[0013] The first dehydrated liquid, which is the filtrate remaining after dehydrating the above slag mixture, can be supplied to the carbon dioxide absorption tower.

[0014] The pH of the first dehydrated solution may be 9 to 13.

[0015] In the above dehydrator, the carbonation slag is washed with process water, and the second dehydration liquid, which is the filtrate remaining after washing, can be supplied to the above cooler.

[0016] The pH of the second dehydrated solution may be 9 to 13.

[0017] It may include a second pipe disposed between the carbon dioxide absorption tower and the carbonation reactor.

[0018] It may include a slag hopper spaced apart on the second pipe and supplying the ironmaking slag to the second pipe.

[0019] The above dehydrator may be at least one selected from the group consisting of a centrifugal dehydrator, a hot air dehydrator, a vacuum dehydrator, a compression dehydrator, a freezing dehydrator, and a drying dehydrator.

[0020] The above dehydrator may include a dehydrator body where a dehydration reaction takes place; a motor disposed on the upper part of the dehydrator body; a dehydration cloth disposed on the inner surface of the dehydrator body; and a scraper disposed spaced apart on the dehydration cloth.

[0021] A mineral carbonation system, which is an embodiment of the present invention, can stably fix carbon dioxide and increase the amount of fixation.

[0022] A mineral carbonation system, which is an embodiment of the present invention, can improve the reaction rate of mineral carbonation.

[0023] A mineral carbonation system, which is one embodiment of the present invention, can remove sulfur components from flue gas without additional chemicals.

[0024] A mineral carbonation system, which is one embodiment of the present invention, can process high pH slag dewatering liquid without a separate neutralization process.

[0025] FIG. 1 is a schematic diagram showing a mineral carbonation system, which is an embodiment of the present invention.

[0026] Figure 2 is a graph showing the change in pH according to the amount of carbon dioxide absorbed in a 1 mol sodium hydroxide solution.

[0027] Figure 3 is a graph showing the change in dissolved carbon dioxide chemical species according to pH.

[0028] Figure 4 is a schematic diagram showing the dehydrator of the present invention.

[0029] FIG. 5 is a schematic diagram showing the carbonation reactor and dehydrator of the present invention.

[0030] Preferred embodiments of the present invention will be described below with reference to the attached drawings. However, embodiments of the present invention may be modified in various other forms, and the scope of the present invention is not limited to the embodiments described below.

[0031] In addition, embodiments of the present invention are provided to more fully explain the present invention to those with average knowledge in the relevant technical field.

[0032] In drawings, the shapes and sizes of elements may be exaggerated for clearer explanation.

[0033] In describing the embodiments of the present invention, if it is determined that a detailed description of known technology related to the present invention may unnecessarily obscure the essence of the present invention, such detailed description will be omitted. Furthermore, the terms described below are defined considering their functions in the present invention, and these may vary depending on the intentions or conventions of the user or operator. Therefore, such definitions should be based on the content throughout this specification. The terms used in the detailed description are merely for describing the embodiments of the present invention and should not be limited in any way. Unless explicitly stated otherwise, expressions in the singular form include the meaning of the plural form.

[0034] In this description, expressions such as “include” or “equipped” are intended to refer to certain characteristics, numbers, steps, actions, elements, parts or combinations thereof, and should not be interpreted to exclude the existence or possibility of one or more other characteristics, numbers, steps, actions, elements, parts or combinations thereof other than those described.

[0035] Unless otherwise specifically defined in the specification of the present invention, % units mean weight %.

[0036] In this specification, terms such as 'top', 'upper', 'upper surface', 'lower', 'lower surface', 'lower surface', and 'side surface' are based on the drawings and may actually vary depending on the direction in which the elements or components are arranged.

[0037] Additionally, throughout the specification, when it is said that one part is 'connected' to another part, this includes not only cases where they are 'directly connected,' but also cases where they are 'indirectly connected' with other elements in between.

[0038] The present invention will be described in detail below through each embodiment or example of the invention. It should be noted that each embodiment or example described in this specification is not limited to a single embodiment or example, but may also be combined with other embodiments or examples. Accordingly, the citation of claims in the patent claims is merely an example of an embodiment, and the technical concept of the present invention should not be interpreted as being limited only to a combination with the cited claims; rather, combinations with various claims are also included within the scope of the technical concept of the present invention.

[0039] One embodiment of the present invention relates to a slag mineral carbonation system (10) using alkali, which may be a technology for selectively absorbing carbon dioxide using alkali and then reacting the solution in which carbon dioxide is dissolved with iron slag to stably fix carbon dioxide. At this time, the mineral carbonation system (10) of one embodiment of the present invention can improve the reaction rate of carbon dioxide fixation and increase the amount of carbon dioxide fixed.

[0040] FIG. 1 is a schematic diagram showing a mineral carbonation system (10) which is an embodiment of the present invention. Referring to FIG. 1, a mineral carbonation system (10) which is an embodiment of the present invention may include a cooler (100) for cooling flue gas; a carbon dioxide absorption tower (200) for absorbing carbon dioxide contained in flue gas; a carbonation reactor (300) for mixing a solution discharged from the carbon dioxide absorption tower (200) with ironmaking slag to carbonate calcium-containing substances in the ironmaking slag; and a dehydrator (400) for dehydrating the slag mixture obtained from the carbonation reactor (300) to obtain carbonated slag.

[0041] The above cooler (100) may be a device for cooling exhaust gas, and more specifically, may be a desulfurization process device for removing sulfur oxides contained in the exhaust gas. The above cooler (100) may be a DCC (Direct Contact Cooler) type cooler (100). The DCC cooler (100) may be a cooling system in which cooling water, such as water, is introduced into the upper part, and the high-temperature gas and the cooling water meet directly within the cooler to lower the temperature of the gas through heat exchange, and the sulfur oxides contained in the exhaust gas react with the cooling water to neutralize them.

[0042] Cooling water can be introduced into the upper part of the cooler (100) and discharged into the lower part of the cooler (100), and exhaust gas can be introduced into the lower part of the cooler (100).

[0043] The exhaust gas introduced into the above cooler (100) is not particularly limited, but, for example, may be exhaust gas containing sulfur oxides (SOx), and may be exhaust gas from a steelmaking process, exhaust gas from a thermal power plant, exhaust gas from a ship, exhaust gas from an automobile, exhaust gas from an oil refinery, etc.

[0044] The above cooling water may be water and may additionally contain an alkaline component. The alkaline component is not particularly limited, but may be, for example, sodium hydroxide (NaOH). The alkaline component contained in the cooling water can remove sulfur oxides contained in the flue gas. The reaction of the alkali to remove sulfur oxides may follow the following formulas (1) to (3).

[0045] [Equation (1)]

[0046] SO2 + NaOH → NaHSO3

[0047] [Essence (2)]

[0048] NaHSO3 + NaOH → Na2SO3 + H2O

[0049] [Essence (3)]

[0050] Na2SO3 + 1 / 2O2 → Na2SO4

[0051] The pH of the cooling water may be 7 to 14, specifically 8 to 13, and more specifically 9 to 13. Sulfur oxides can be removed more effectively within the above-described pH range.

[0052] The temperature of the cooling water introduced into the cooler (100) is not particularly limited, but, for example, may be 25 to 50°C.

[0053] A mineral carbonation system (10) which is an embodiment of the present invention may include a cooling tower (110) that supplies cooling water to the cooler (100). The cooling tower (110) not only supplies cooling water to the cooler (100) but can also store cooling water discharged from the cooler (100) and can also receive cooling water discharged from the cooler (100) to cool it again.

[0054] The cooling tower (110) can cool the water supplied to the cooler (100). The cooling method of the cooling tower (110) may be a cooling means commonly used in the industry.

[0055] It may include a first pipe (120) that supplies cooling water to the top of the cooler (100). Additional cooling water may be supplied through the first pipe (120).

[0056] The carbon dioxide absorption tower (200) above may be a device that absorbs and removes carbon dioxide contained in flue gas. The carbon dioxide absorption reaction in the carbon dioxide absorption tower (200) may be a reaction according to the following equations (4) to (6).

[0057] [Equation (4)]

[0058] CO2 + H2O → H2CO3

[0059] [Essence (5)]

[0060] H2CO3 + OH - → H2O + HCO3 -

[0061] [Essence (6)]

[0062] HCO3 - + OH - → H2O + CO3 2-

[0063] The carbon dioxide absorption tower (200) can absorb carbon dioxide using a carbon dioxide absorption liquid, and the carbon dioxide absorption liquid may contain an alkaline component. The alkaline component is not particularly limited, but may be, for example, sodium hydroxide (NaOH).

[0064] The carbon dioxide absorption liquid may include a first dewatering liquid discharged from a dewatering machine (400) to be described later. By including the first dewatering liquid in the carbon dioxide absorption liquid, the dewatering liquid generated after slag dewatering can be easily reused.

[0065] The pH of the absorption solution may be 7 to 14, specifically 8 to 13, and more specifically 9 to 13. Carbon dioxide contained in the flue gas can be removed more effectively within the above-described pH range. The flue gas discharged from the cooler (100) may be introduced into the lower part of the carbon dioxide absorption tower (200), and the solution from which carbon dioxide has been removed may be discharged from the bottom of the carbon dioxide absorption tower (200). The flue gas from which carbon dioxide has been removed may be discharged from the top of the carbon dioxide absorption tower (200). The carbon dioxide absorption solution may be introduced into the upper part of the carbon dioxide absorption tower (200).

[0066] It may include a second pipe (210) disposed between the carbon dioxide absorption tower (200) and the carbonation reactor (300). A solution that has absorbed carbon dioxide can be supplied from the second pipe (210) to the carbonation reactor (300).

[0067] The carbonation reactor (300) may be a device that carbonates the calcium-containing material in the steel slag by mixing steel slag with the solution that has absorbed carbon dioxide in the carbon dioxide absorption tower (200).

[0068] The above iron slag may contain a calcium-containing material, and the calcium-containing material may react with carbonate ions or bicarbonate ions contained in a solution that has absorbed carbon dioxide to produce calcium carbonate and a carbonation reaction that regenerates alkali may occur, and a slag mixture may be obtained.

[0069] The above carbonation reaction may be a reaction according to the following formula (7) or formula (8).

[0070] [Essence (7)]

[0071] CaO + CO3 2- + H2O → CaCO3 + 2OH -

[0072] [Essence (8)]

[0073] CaO + HCO3 - → CaCO3 + OH -

[0074] The above iron slag may be slag generated in at least one process selected from a blast furnace, a converter, etc., and may have a calcium-containing material content of 10 to 50 weight%. The calcium-containing material may be calcium oxide (CaO).

[0075] It may include a slag hopper (310) spaced apart from the second pipe (210) and supplying the steelmaking slag to the second pipe (210). The steelmaking slag may be mixed with a solution containing carbon dioxide before being supplied to the second pipe (210) and introduced into the carbonation reactor (300).

[0076] Figure 2 is a graph showing the change in pH according to the amount of carbon dioxide absorbed in a 1 molar sodium hydroxide solution. Figure 3 is a graph showing the change in dissolved carbon dioxide chemical species according to pH. Referring to Figures 2 and 3, the pH of the rich solution (α=0.7~1.0) used in the mineral carbonation process is approximately 7.9 to 9.2, while the pH of the lean solution (α=0.5~0.7) is approximately 9.2 to 11.4, indicating a high pH. In particular, in the case of slag slurry, under the conditions of a lean solution, the water (pore water) contained in the slag also exhibits a high pH, ​​resulting in the slag dewatering liquid having a pH of 9.2 to 11.4. In this case, it is necessary to adjust the pH to 6.0 to 8.5 through neutralization before discharging the dewatering liquid.

[0077] Accordingly, one embodiment of the present invention includes a dehydrator (400) to separate the dehydrated liquid, and by not discharging the separated dehydrated liquid, it is not necessary to have a separate pH adjustment process, and by recycling the dehydrated liquid as a carbon dioxide absorption liquid and / or cooling water, economic efficiency can be achieved.

[0078] FIG. 4 is a schematic diagram showing the dehydrator (400) of the present invention. Referring to FIG. 4, the dehydrator (400) may be a device for obtaining carbonated slag (CS) by dehydrating the slag mixture obtained from the carbonation reactor (300).

[0079] The above dehydrator (400) may be at least one selected from the group consisting of, for example, a centrifugal dehydrator, a hot air dehydrator, a vacuum dehydrator, a compression dehydrator, a freezing dehydrator, and a drying dehydrator.

[0080] The above dehydrator (400) may include: a dehydrator body (401) where a dehydration reaction occurs; a motor (402) disposed on the upper part of the dehydrator body (401); a dehydration cloth (403) disposed on the inner side of the dehydrator body (401); and a scraper (404) disposed spaced apart on the dehydration cloth (403).

[0081] The dewatering method of the above dewatering machine (400) may be as follows. First, a slag mixture may be introduced into the main body (401) of the above dewatering machine. The motor (402) may rotate the dewatering machine (400) into which the slag mixture has been introduced to dewater the slag mixture into carbonated slag. The dewatered carbonated slag may be placed on the dewatering cloth (403), and the carbonated slag may be obtained and the first dewatering liquid, which is the dewatering filtrate, may be obtained. Afterward, the carbonated slag may be washed with process water and the remaining second dewatering liquid may be obtained. After the washing is finished, the carbonated slag remaining on the dewatering cloth (403) may be obtained using a scraper (404).

[0082] The carbonated slag obtained according to the above method can be removed by a carbon dioxide absorption solution and is of excellent quality, and can be recycled for various uses such as construction materials, soil conditioners, and road paving materials.

[0083] The pH of the first dehydrated liquid may be equal to or higher than the pH of the second dehydrated liquid. The pH of each of the first dehydrated liquid and the second dehydrated liquid may increase during the carbonation process. Specifically, the pH of the first dehydrated liquid may be 9 to 13, and the pH of the second dehydrated liquid may be 9 to 13. The first dehydrated liquid can easily remove carbon dioxide within the aforementioned pH range, and the second dehydrated liquid can easily remove sulfur oxides within the aforementioned pH range.

[0084] It may include a third pipe (320) disposed between the carbonation reactor (300) and the dehydrator (400). A solution from which carbon dioxide has been removed may be supplied through the third pipe (320). Referring to FIG. 4, the third pipe (320) may be connected to the interior of the dehydrator body (401) to supply the solution remaining after carbon dioxide has been removed.

[0085] Additionally, the dewatering unit (400) can dewater the slag mixture obtained from the carbonation reactor (300) to obtain carbonation slag and supply the first dewatered liquid, which is the dewatered liquid, to the carbon dioxide absorption tower (200). In one embodiment of the present invention, the amount of carbon dioxide absorption liquid used in the carbonation process can be saved by recycling the first dewatered liquid, which is a high pH dewatered liquid, as a carbon dioxide absorption liquid.

[0086] Furthermore, the dehydrator (400) can wash the carbonation slag with process water and supply the remaining second dehydration liquid to the cooler (100). The second dehydration liquid can discharge carbonation slag with a pH adjusted by including alkaline components remaining in the carbonation slag, and the second dehydration liquid can be used as cooling water for the cooler (100) to achieve economic efficiency.

[0087] Since the pH of the first dehydrated liquid may be equal to or higher than the pH of the second dehydrated liquid, if the second dehydrated liquid is supplied to the carbon dioxide absorption tower (200) in the same way as the first dehydrated liquid, the pH of the carbon dioxide absorption liquid may decrease, and a problem may arise in which additional dehydrated liquid must be supplied.

[0088] The above dehydrator (400) may include a process water supply unit (410) that supplies the process water. The process water is not subject to any particular limitations, but may be, for example, water (H2O).

[0089] It may include a fifth pipe (430) that supplies the second dehydrated liquid to the first pipe (120). Since the second dehydrated liquid may already be in a cooled state, it can be supplied directly to the first pipe (120) without additional cooling and introduced into the cooler (100).

[0090] In another embodiment, the fifth pipe (430) can be directly connected to the cooler (100).

[0091] FIG. 5 is a schematic diagram showing the carbonation reactor (300) and dehydrator (400) of the present invention. Referring to FIG. 5, it can be seen that the carbonation slag discharged from the dehydrator (400) is discharged separately, and the first dehydration liquid and the second dehydration liquid discharged from the dehydrator (400) are recycled rather than being discharged as wastewater.

[0092] Additionally, referring to FIGS. 1 and FIGS. 5, one embodiment of the present invention may include a first dehydrated liquid storage tank (500) for storing the first dehydrated liquid. The first dehydrated liquid may be stored in the first dehydrated liquid storage tank (500) and then supplied to the carbon dioxide absorption tower (200) as needed.

[0093] It may include a sixth pipe (520) disposed between the first dehydrated liquid storage tank (500) and the carbon dioxide absorption tower (200). The first dehydrated liquid may be supplied through the sixth pipe (520).

[0094] Additionally, it may include a supplementary tank (510) that supplies carbon dioxide absorption liquid to the sixth pipe (520). The supplementary tank (510) can adjust the pH of the first cleaning liquid introduced into the carbon dioxide absorption tower (200) as needed.

[0095] It may include a seventh pipe disposed between the first dehydrated liquid storage tank and the dehydrater. The seventh pipe (530) may supply the first dehydrated liquid to the third pipe (320).

[0096] It may include a first pump (610) disposed on the second pipe (210). The first pump (610) can easily transport the carbon dioxide-removed solution, which is the feed supplied from the carbon dioxide absorption tower (200) to the carbonation reactor (300).

[0097] It may include a third pump (630) disposed on the fifth pipe (430). The third pump (630) can easily transport the second dehydrated liquid, which is the supply supplied from the dehydrater (400) to the cooler (100).

[0098] It may include a second pump (620) disposed on the sixth pipe (520). The second pump (620) can easily transport the first dehydrated liquid, which is the feed supplied from the dehydrater (400) to the carbon dioxide absorption tower (200).

[0099] Although embodiments of the present invention have been described in detail above, the scope of the present invention is not limited thereto, and it will be obvious to those skilled in the art that various modifications and variations are possible within the scope of the technical concept of the present invention as described in the claims.

[0100] [Explanation of the symbol]

[0101] 10: Mineral carbonation system 100: Cooler

[0102] 110: Cooling Tower 120: 1st Pipe

[0103] 200: Carbon dioxide absorption tower 210: Second pipe

[0104] 300: Carbonation reactor 310: Slag hopper

[0105] 320: 3rd pipe 400: Dehydrator

[0106] 401: Dehydrator body 402: Motor

[0107] 403: Dehydrated blister 404: Scraper

[0108] 410: Process water supply unit 420: Piping 4

[0109] 430: Piping No. 5 500: Dehydrated Liquid Storage Tank No. 1 510: Replenishment Tank

[0110] 520: Pipe No. 6 530: Pipe No. 7

[0111] 610: Pump 1 620: Pump 2

[0112] 630: Third pump

Claims

1. A cooler for cooling exhaust gas; A carbon dioxide absorption tower that absorbs carbon dioxide contained in flue gas; A carbonation reactor for mixing the solution discharged from the above-mentioned carbon dioxide absorption tower with ironmaking slag to carbonate calcium-containing substances in the ironmaking slag; and A mineral carbonation system comprising a dehydrator for obtaining carbonated slag by dehydrating a slag mixture obtained from the above carbonation reactor.

2. In Paragraph 1, A mineral carbonation system comprising a first pipe that supplies cooling water to the top of the cooler.

3. In Paragraph 1, A mineral carbonation system in which the first dehydrated liquid, which is the filtrate remaining after dehydrating the above slag mixture, is supplied to the above carbon dioxide absorption tower.

4. In Paragraph 3, A mineral carbonation system in which the pH of the first dehydrated liquid is 9 to 13.

5. In Paragraph 1, A mineral carbonation system in which carbonation slag is washed with process water in the above-mentioned dehydrator, and the second dehydration liquid remaining after washing is supplied to the above-mentioned cooler.

6. In Paragraph 5, A mineral carbonation system in which the pH of the second dehydrated liquid is 9 to 13.

7. In Paragraph 1, A mineral carbonation system comprising a second pipe disposed between the carbon dioxide absorption tower and the carbonation reactor.

8. In Paragraph 7, A mineral carbonation system comprising a slag hopper spaced apart on the second pipe and supplying the ironmaking slag to the second pipe.

9. In Paragraph 1, The above dehydrator is at least one selected from the group consisting of a centrifugal dehydrator, a hot air dehydrator, a vacuum dehydrator, a compression dehydrator, a freezing dehydrator, and a drying dehydrator, in a mineral carbonation system.

10. In Paragraph 1, The above dehydrator is, Dehydrator body where the dehydration reaction takes place; A motor positioned on the upper part of the above-mentioned dehydrator body; A dehydration cloth disposed on the inner surface of the main body of the dehydrator; and A mineral carbonation system comprising a scraper spaced apart and disposed on the above dehydration blister.

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