Method for manufacturing carbonated binder, deep cement mixing method for improving soft ground using same, carbon dioxide-utilizing deep cement mixing soft ground improvement body produced thereby, method for manufacturing carbonated binder-containing concrete using same, concrete member manufactured thereby, carbonation reaction apparatus used in method for manufacturing carbonated binder, and carbon dioxide capture device using carbonation reaction apparatus

Abstract

The present invention relates to a method for manufacturing a carbonated binder using carbon dioxide for treating captured carbon dioxide, a deep cement mixing method for improving soft ground using same, a carbonation reaction apparatus used in the method for manufacturing a carbonated binder, and a carbon dioxide capture device using the carbonation reaction apparatus. The method for manufacturing the carbonated binder comprises: (a) mixing a powdered binder with mixing water to generate a liquid mixed binder; and (b) reacting the generated liquid mixed binder with carbon dioxide by means of a carbonation reaction apparatus to produce a carbonated binder, wherein the carbonation reaction apparatus may be configured to operate in a continuous flow manner in which the liquid mixed binder is sequentially introduced, reacted with carbon dioxide, and discharged.

Description

A method for manufacturing a carbonation binder, a deep mixing treatment method for soft ground improvement using the same, a soft ground improvement material treated with deep mixing utilizing carbon dioxide generated therefrom, a method for manufacturing concrete containing a carbonation binder using the same, a concrete member manufactured thereby, a carbonation reaction device used in the method for manufacturing a carbonation binder, and a carbon dioxide capture device using the carbonation reaction device.

[0001] The present invention relates to a method for manufacturing a carbonation binder, a deep mixing treatment method for improving soft ground using the same, a soft ground improvement material using deep mixing treatment utilizing carbon dioxide generated through the same, a method for manufacturing concrete including a carbonation binder using the same, a concrete member manufactured by the same, a carbonation reaction device used in the method for manufacturing a carbonation binder, and a carbon dioxide capture device using the carbonation reaction device.

[0002] In particular, the present invention relates to a method for manufacturing a carbonation binder using carbon dioxide for the treatment of captured carbon dioxide, a carbon dioxide capture device using a carbonation reaction apparatus, etc., and corresponds to green technologies directly related to carbon dioxide capture, such as technologies for the treatment and permanent sequestration of captured carbon dioxide and technologies for constructing facilities to capture emitted carbon dioxide.

[0003] To address the issue of climate change, the international community adopted the United Nations Framework Convention on Climate Change in 1992 and imposed national obligations to reduce greenhouse gas emissions through the Kyoto Protocol in 1997, but failed to implement them. It was only after the Paris Agreement was adopted that reduction obligations were imposed on all 195 parties, leading to the establishment of greenhouse gas reduction targets.

[0004] It is predicted that the tipping point for the rise in global average temperature will be between 1.5°C and 2.0°C. Based on this prediction, the Paris Agreement entered into force under the global long-term goal of limiting the rise in global average temperature to within 1.5°C compared to pre-industrial levels, and many countries have declared and legislated carbon neutrality (Net-Zero) to implement it.

[0005] Carbon Capture, Utilization, and Storage (CCUS) technology includes CCS technology for capturing and storing carbon dioxide, and CCU technology for capturing and utilizing it.

[0006] Cement is a formidable enemy of carbon neutrality because it emits 1 ton of carbon dioxide for every ton of cement produced. The cement industry accounts for 5–9% of total carbon dioxide emissions. Furthermore, it has been found that the annual carbon dioxide emissions from the global cement industry have tripled over the past 20 years. In the case of the South Korean cement industry, annual carbon dioxide emissions gradually increased from 15.87 million tons in 1990 to 24.92 million tons in 2019.

[0007] Reducing cement usage and developing alternative materials is the fastest way for the construction sector to meet the contemporary challenge of responding to the climate crisis.

[0008] The technology forming the background of the present invention is disclosed in Korean Published Patent Application No. 10-2021-0125991.

[0009] The present invention aims to solve the problems of the aforementioned conventional technology by reducing the amount of carbon dioxide and cement used by utilizing (treating) captured carbon dioxide, and to provide a method for manufacturing a carbonation binder that can replace cement, a deep mixing treatment method for soft ground improvement using the same, a soft ground improvement material produced by deep mixing treatment utilizing carbon dioxide generated through the same, a method for manufacturing concrete including a carbonation binder using the same, a concrete member manufactured by the same, a carbonation reaction device used in the method for manufacturing the carbonation binder, and a carbon dioxide capture device using the carbonation reaction device.

[0010] However, the technical problems that the embodiments of the present invention aim to solve are not limited to the technical problems described above, and other technical problems may exist.

[0011] As a technical means for achieving the above-mentioned technical problem, a method for manufacturing a carbonation binder according to the first aspect of the present invention comprises: (a) a step of mixing a powdered binder with water to produce a liquid mixed binder; and (b) a step of producing a carbonation binder by reacting the produced liquid mixed binder with carbon dioxide using a carbonation reaction device, wherein the carbonation reaction device may be provided to follow a continuous flow method in which the flow of the liquid mixed binder being introduced, reacted with carbon dioxide, and discharged is carried out sequentially.

[0012] In addition, in step (a) above, the liquid mixed binder may be produced to include a powdered binder with a fineness of 2,000 cm2 / g (Blaine) or more, and a mixed water with a weight ratio of water to the powdered binder of 70% or more and 120% or less, taking into account the flow in the continuous flow method of step (b).

[0013] In addition, in step (b) above, a liquid carbon dioxide storage tank, a vaporizer, and a pressure reducing device are connected to the carbonation reaction device so that gaseous carbon dioxide can be injected.

[0014] In addition, the pressure reducing device includes a carbon dioxide buffer storage tank for buffering and storing the reduced-pressure gaseous carbon dioxide, and the carbon dioxide buffer storage tank may be configured to maintain a pressure within a preset pressure range.

[0015] Additionally, the carbonation reaction device may include: an input section into which a liquid mixed binder is introduced; a main body into which the introduced liquid mixed binder reacts with CO2 (a main body that reacts with CO2 by maximizing the specific surface area of ​​the introduced liquid mixed binder); a discharge section having a discharge port into which at least a portion of the reacted liquid mixed binder is discharged; and a carbon dioxide injection section for injecting carbon dioxide into the main body.

[0016] Additionally, the input section includes an input port connected to the main body, a transfer pipe connected to the input port, and a pump provided to apply pressure to inject a liquid mixing binder into the main body, wherein the input port is closed by the injected liquid mixing binder and the discharge port is closed by the discharged liquid mixing binder, so that the interior of the main body is controlled to follow the continuous flow method while maintaining a closed state that is closed above a preset level.

[0017] Additionally, in step (b) above, due to the vacuum phenomenon caused by the carbonation reaction between the liquid mixed binder and carbon dioxide inside the main body, a negative pressure corresponding to at least a portion of the pressure required to inject carbon dioxide into the main body may be formed in the carbon dioxide injection part.

[0018] In addition, the main body may include a static mixer section comprising a static mixer provided inside the passage to induce turbulent mixing for a liquid mixed binder discharged to the discharge section connected to the other side, passing through a passage directly or indirectly connected to one side of the input section and the carbon dioxide injection section.

[0019] Additionally, the main body may include a venturi tube section provided in the form of a venturi tube, the input section is connected to one side of the venturi tube, the discharge section is connected to the other side of the venturi tube, and the carbon dioxide injection section may be provided to be located closer to the minimum cross-section position among the position where the passage cross-section of the tube is the maximum cross-section and the position where the minimum cross-section is the minimum cross-section in the venturi tube.

[0020] Additionally, the main body may include a venturi tube section portion configured in the form of a venturi tube, with one side connected to the input portion and the carbon dioxide injection portion connected in the middle; and a static mixer section portion configured in the form of a static mixer, with one side connected to the other side of the venturi tube section portion and the other side connected to the discharge portion.

[0021] Additionally, the main body may include a venturi tube section formed in the shape of a venturi tube, with one side connected to the input section and the carbon dioxide injection section connected in the middle; and a turbulent mixing section, with one side connected to the other side of the venturi tube section and the other side connected to the discharge section, and a chamber formed in the middle to induce turbulent mixing.

[0022] In addition, the main body may include a stirring device that stirs the liquid mixed binder, which is discharged to the discharge part connected to the other side through a passage directly or indirectly connected to the input part and the carbon dioxide injection part on one side, at a high speed to increase the reaction contact surface with the carbon dioxide.

[0023] Additionally, the discharge portion of the carbonation reaction device is connected to a carbon dioxide recovery device, and the carbon dioxide recovery device may include a carbon dioxide separation chamber connected to the discharge portion and extending downward; and a carbon dioxide recovery portion connected to the upper side of the carbon dioxide separation chamber.

[0024] In addition, the carbonation reaction device may be provided such that a plurality of unit carbonation reaction devices are arranged in series, a plurality of unit carbonation reaction devices are arranged in parallel, or a plurality of unit carbonation reaction devices are arranged in a matrix form that combines series and parallel.

[0025] In addition, the total length of the carbonation reaction device may be set to have a flow rate difference that maintains a continuous fluid flow with friction in a state where the carbon dioxide reaction proceeds beyond a preset reaction amount, taking into account the vacuum phenomenon that occurs during the reaction with carbon dioxide.

[0026] In addition, the carbonation reaction device comprises a plurality of unit devices connected in series, and the unit devices comprise a carbon dioxide injection unit and a static mixer, and the length of each unit reaction device may be set to have a flow rate difference such that a continuous fluid flow considering friction is maintained at a flow rate when the carbon dioxide reaction proceeds beyond a preset reaction amount.

[0027] Meanwhile, a method for manufacturing a carbonation binder according to the second aspect of the present invention comprises: (a) a step of mixing a powdered binder with water to produce a liquid mixed binder; and (b) a step of producing a carbonation binder by reacting the produced liquid mixed binder with carbon dioxide using a carbonation reaction device, wherein the carbonation reaction device comprises: a binder chamber including a first input section into which the produced liquid mixed binder is introduced and a first discharge section for discharging at least a partially reacted liquid mixed binder; and a circulation transfer device connected to the binder chamber and including a reaction section in which the introduced liquid mixed binder reacts with carbon dioxide, provided to follow a circulation flow method in which the liquid mixed binder contained in the binder chamber repeatedly passes through the reaction section, and carbon dioxide may be supplied to the reaction section by a carbon dioxide injection section connected to the circulation transfer device.

[0028] In addition, in step (a) above, the liquid mixed binder may be produced by considering the flow rate in the circulating flow method of step (b) above, and may include a powdered binder with a fineness of 2,000 cm2 / g (Blaine) or more and a pH of 10 or more, and a mixed water with a weight ratio of 50% or more to the powdered binder.

[0029] In addition, in step (b) above, the circulating transfer device may be connected to a liquefied carbon dioxide storage tank, a vaporizer, and a pressure reducing device so that gaseous carbon dioxide can be injected.

[0030] In addition, the pressure reducing device includes a carbon dioxide buffer storage tank for buffering and storing the reduced-pressure gaseous carbon dioxide, and the carbon dioxide buffer storage tank may be configured to maintain a pressure within a preset pressure range.

[0031] Additionally, the above-described circulation transfer device may include: a reaction section; an inlet section connected to the binder chamber and into which the liquid mixed binder is introduced from the binder chamber; and a transfer pipe provided to allow the liquid mixed binder introduced into the inlet section to move toward the reaction section, wherein the reaction section may include: a second input section connected to the transfer pipe and into which the liquid mixed binder that has moved along the transfer pipe is introduced; a main body into which the introduced liquid mixed binder reacts with carbon dioxide; and a second discharge section into which at least a portion of the reacted liquid mixed binder is discharged to the binder chamber.

[0032] Additionally, the carbon dioxide injection unit for directly or indirectly injecting carbon dioxide into the reaction unit is connected to the circulation transfer device, and the carbon dioxide recovery pipe may be connected to the binder chamber so that the carbon dioxide injected from the carbon dioxide injection unit that has not reacted with the liquid mixed binder is recovered into the carbon dioxide buffer storage tank.

[0033] Additionally, the inlet may include an inlet connected to the binder chamber and a pump provided to apply pressure to introduce the liquid mixed binder into the reaction section.

[0034] Additionally, the pump may be a venturi pump provided to inject the carbon dioxide at a pressure above a preset pressure and to apply pressure such that the liquid mixed binder is injected into the main body through the vacuum generated by the injection of carbon dioxide at a pressure above the preset pressure.

[0035] Additionally, the main body may include a static mixer section comprising a static mixer provided inside the passage to induce turbulent mixing for a liquid mixed binder discharged to the second discharge section connected to the other side, passing through a passage directly or indirectly connected to one side of the second input section and the carbon dioxide injection section.

[0036] Additionally, the main body may include a venturi tube section provided in the form of a venturi tube, the second input section is connected to one side of the venturi tube, the second discharge section is connected to the other side of the venturi tube, and the carbon dioxide injection section may be provided to be located closer to the minimum cross-section position among the position where the passage cross-section of the tube is the maximum cross-section and the position where the minimum cross-section is the minimum cross-section in the venturi tube.

[0037] Additionally, the second discharge section is connected so that the liquid mixed binder discharged therefrom forms a spiral flow that proceeds spirally along the direction of gravity within the binder chamber, and the inlet section may be connected to the binder chamber at a lower side than the second discharge section to implement the circulation flow method.

[0038] Additionally, the binder chamber is provided in a cone shape with a diameter that decreases toward the bottom, and the second discharge part may be connected to the inside of the binder chamber so that a liquid mixed binder that has reacted at least partially with carbon dioxide is discharged in the circumferential direction of the binder chamber or in the tangential direction thereof.

[0039] In addition, the carbonation reaction device further includes a temperature measuring device for measuring the temperature inside the binder chamber, and can control the number of times the liquid mixed binder repeatedly passes through the reaction section based on the temperature measured by the temperature measuring device.

[0040] In addition, the carbonation reaction device further includes a flow meter capable of measuring the amount of carbon dioxide injected by the carbon dioxide injection part, and can control the number of times the liquid mixed binder repeatedly passes through the reaction part based on the amount of carbon dioxide injected measured through the flow meter.

[0041] In addition, the carbonation reaction device may be provided in multiple units, the carbon dioxide buffer storage tank may be provided to be shared with the multiple carbonation reaction devices, the first discharge portion of each of the multiple carbonation reaction devices may be connected, and the multiple carbonation reaction devices may be provided in an alternating circulation method that alternately discharges the carbonation binder in the order in which the manufacture of the carbonation binder is completed.

[0042] Meanwhile, a deep mixing treatment method for improving soft ground according to the third aspect of the present invention may include: (a) a step of manufacturing a carbonation binder by a carbonation binder manufacturing method according to the first or second aspect of the present invention; (b) a step of manufacturing a carbonation mixture by mixing the carbonation binder with original ground soil; and (c) a step of curing the carbonation mixture to produce a soft ground improvement body.

[0043] Meanwhile, the soft ground improvement material using deep mixing treatment with carbon dioxide according to the fourth aspect of the present invention can be produced by the deep mixing treatment method for soft ground improvement according to the third aspect of the present invention.

[0044] Meanwhile, a method for manufacturing concrete comprising a carbonation binder according to the fifth aspect of the present invention may include: (a) a step of manufacturing a carbonation binder by a method for manufacturing a carbonation binder according to the first or second aspect of the present invention; and (b) a step of manufacturing concrete by stirring the manufactured carbonation binder with aggregate.

[0045] Meanwhile, a concrete member using carbon dioxide according to the sixth aspect of the present invention can be manufactured by a method for manufacturing concrete comprising a carbonation binder according to the fifth aspect of the present invention.

[0046] Meanwhile, a carbonation reaction device according to the seventh aspect of the present invention comprises: a binder chamber including a first input section into which a liquid mixed binder is introduced and a first discharge section for discharging at least a partially reacted liquid mixed binder; and a circulation transfer device connected to the binder chamber and including a reaction section in which the introduced liquid mixed binder reacts with carbon dioxide, wherein the carbonation reaction device is provided to follow a circulation flow method in which the liquid mixed binder contained in the binder chamber repeatedly passes through the reaction section, and carbon dioxide may be supplied to the reaction section by a carbon dioxide injection section connected to the circulation transfer device.

[0047] Meanwhile, a carbon dioxide capture device according to the eighth aspect of the present invention comprises: an absorbent chamber including a first input section into which a liquid carbon dioxide absorbent is introduced and a first discharge section for discharging at least a partially reacted liquid carbon dioxide absorbent; and a circulation transfer device connected to the absorbent chamber and including a reaction section in which the introduced liquid carbon dioxide absorbent reacts with carbon dioxide of a carbon dioxide-containing gas, wherein the carbon dioxide capture device is provided to follow a circulation flow method in which the liquid carbon dioxide absorbent contained in the absorbent chamber repeatedly passes through the reaction section, and a carbon dioxide-containing gas may be injected into the reaction section by a carbon dioxide-containing gas injection section connected to the circulation transfer device.

[0048] In addition, the carbon dioxide-containing gas may be air or exhaust gas.

[0049] The means for solving the problem described above are merely exemplary and should not be interpreted as intended to limit the present invention. In addition to the exemplary embodiments described above, additional embodiments may exist in the drawings and the detailed description of the invention.

[0050] According to the means for solving the problem of the present invention described above, by reacting a liquid mixed binder with carbon dioxide through a carbonation reaction device to produce a carbonation binder, it is possible to continuously produce a carbonation binder utilizing carbon dioxide with a constant flow rate.

[0051] According to the means for solving the problem of the present invention described above, by reacting a liquid mixed binder with carbon dioxide through a carbonation reaction device to produce a carbonation binder, it is possible to produce a carbonation binder using carbon dioxide.

[0052] According to the means for solving the problem of the present invention described above, carbon neutrality can be contributed by utilizing and storing captured carbon dioxide.

[0053] According to the solution to the problem of the present invention described above, carbon neutrality can be contributed to by suppressing the generation of carbon dioxide by reducing the use of cement.

[0054] According to the solution to the problem described above, by utilizing carbon dioxide to increase the strength of soft ground improvement materials, the amount of binder used is reduced. Consequently, costs for transportation and storage are lowered due to the reduced binder usage. Additionally, carbon dioxide emissions generated during cement production are reduced, carbon dioxide emissions during transportation are lowered due to the reduced amount of binder transported, and additional carbon credits are used to enhance economic efficiency and environmental sustainability in various aspects.

[0055] However, the effects obtainable from this invention are not limited to those described above, and other effects may exist.

[0056] FIG. 1 is a flowchart of a method for manufacturing a carbonated binder according to the first aspect of the present invention or the second aspect to be described later.

[0057] Figure 2 is a diagram illustrating the approximate composition ratios of CaO and MgO in materials corresponding to the powdered binder.

[0058] Figure 3a is a photograph of a carbon dioxide reaction experiment using a PET bottle conducted at this institution, and Figure 3b is a photograph of a phenolphthalein color change conducted at this institution.

[0059] Figure 4 is a schematic diagram of the carbon dioxide reaction amount measurement test using a balloon conducted at this institution.

[0060] FIG. 5 is a drawing for explaining the case where the main body of a carbonation reaction device includes a static mixer section in the first aspect of the present invention.

[0061] FIG. 6 is a drawing for explaining a static mixer in the first aspect of the present invention.

[0062] FIG. 7 is a drawing for explaining the case where the main body of a carbonation reaction device includes a venturi tube section in the first aspect of the present invention.

[0063] FIG. 8a is a drawing for explaining a single venturi tube in the first aspect of the present invention, and FIG. 8b is a drawing for explaining a multi-venturi tube.

[0064] FIG. 9 is a drawing for explaining the case in which the main body of a carbonation reaction device includes a venturi tube section and a static mixer section in the first aspect of the present invention.

[0065] FIG. 10 is a drawing for explaining the case in which the main body of a carbonation reaction device includes a turbulent mixing section in the first aspect of the present invention.

[0066] FIG. 11 is a drawing illustrating the appearance of a stirring device provided on the main body of a carbonation reaction device in the first aspect of the present invention.

[0067] FIG. 12 is a drawing for explaining a case in which, in the first aspect of the present invention, a carbon dioxide recovery unit is provided at the top of the main body of a carbonation reaction device and a carbon dioxide injection unit is provided at the bottom of the main body.

[0068] FIG. 13 is a drawing for explaining the case of dispersing and injecting carbon dioxide in the first aspect of the present invention.

[0069] FIG. 14 is a drawing for explaining a carbon dioxide recovery device in the first aspect of the present invention.

[0070] FIG. 15a is a drawing for explaining the overall length of a carbonation reaction apparatus in the first aspect of the present invention, FIG. 15b is a drawing for explaining another embodiment in which a pipe diameter design is made considering the gradient of vacuum phenomenon progression in the first aspect of the present invention, and FIG. 15c is a drawing for explaining a plurality of unit devices in the first aspect of the present invention.

[0071] FIG. 16 is a drawing for explaining step S12 in the second aspect of the present invention.

[0072] FIG. 17 is a drawing for explaining a binder chamber configured to allow a liquid mixed binder to flow spirally in the second aspect of the present invention or in the seventh aspect to be described later.

[0073] Fig. 18 is a cross-sectional view of AA of Fig. 17.

[0074] FIGS. 19 and 20 are drawings for explaining the case where the reaction section of a carbonation reaction device includes a static mixer section in the second aspect of the present invention or the seventh aspect to be described later.

[0075] FIG. 21 is a drawing for explaining a static mixer in the second aspect of the present invention or in the seventh aspect to be described later.

[0076] FIGS. 22 and 23 are drawings for explaining the case where the reaction section of the carbonation reaction device includes a venturi tube section in the second aspect of the present invention or the seventh aspect to be described later.

[0077] FIG. 24 is a drawing for explaining the Venturi tube section in the second aspect of the present invention or in the seventh aspect to be described later.

[0078] FIG. 25 is a drawing for explaining a multi-venturi tube in the second aspect of the present invention or in the seventh aspect to be described later.

[0079] FIGS. 26 and 27 are drawings for explaining the case in which the reaction section of a carbonation reaction device includes a venturi tube section and a static mixer section in the second aspect of the present invention or the seventh aspect to be described later.

[0080] FIGS. 28 and 29 are drawings for explaining the case where the pump is equipped as a venturi pump in the second aspect of the present invention or in the seventh aspect to be described later.

[0081] FIG. 30 is a drawing for explaining the case where a plurality of carbonation reaction devices are provided in the second aspect of the present invention or in the seventh aspect to be described later.

[0082] FIG. 31 is a flowchart of a deep mixing treatment method for soft ground improvement according to the third aspect of the present invention.

[0083] Figure 32 is a drawing to explain the results of comparing the strength of a carbonated DCM mold to which the present invention is applied and a general DCM mold.

[0084] FIG. 33 is a flowchart of a method for manufacturing concrete containing a carbonation binder according to the fifth aspect of the present invention.

[0085] FIG. 34 is a drawing for explaining a carbon dioxide capture device using a carbonation reaction device according to the eighth aspect of the present invention.

[0086] Embodiments of the present invention are described below with reference to the attached drawings to enable those skilled in the art to easily implement the invention. However, the present invention may be embodied in various different forms and is not limited to the embodiments described herein. Furthermore, in order to clearly explain the present invention in the drawings, parts unrelated to the explanation have been omitted, and similar parts throughout the specification are denoted by similar reference numerals.

[0087] Throughout this specification, when a part is described as being "connected" to another part, this includes not only cases where they are "directly connected," but also cases where they are "electrically connected" or "indirectly connected" with other elements interposed between them.

[0088] Throughout the entire specification, when a component is described as being located "on," "on top," "on top," "under," "on bottom," or "on bottom" of another component, this includes not only cases where the component is in contact with the other component but also cases where another component exists between the two components.

[0089] Throughout this specification, when a part is described as "comprising" a certain component, this means that, unless specifically stated otherwise, it does not exclude other components but may include additional components.

[0090] The present invention relates to a method for manufacturing a carbonation binder, a deep mixing treatment method for improving soft ground using the same, a soft ground improvement material using deep mixing treatment utilizing carbon dioxide generated through the same, a method for manufacturing concrete including a carbonation binder using the same, a concrete member manufactured by the same, a carbonation reaction device used in the method for manufacturing a carbonation binder, and a carbon dioxide capture device using the carbonation reaction device.

[0091] <Method for manufacturing a carbonation binder according to the first aspect of the present invention>

[0092] Hereinafter, a method for manufacturing a carbonation binder according to the first aspect of the present invention (hereinafter referred to as the 'present manufacturing method (S1)') will be described.

[0093] FIG. 1 is a flowchart of a method for manufacturing a carbonated binder according to the first aspect of the present invention or the second aspect to be described later.

[0094] Figure 2 is a diagram illustrating the approximate composition ratios of CaO and MgO in materials corresponding to the powdered binder.

[0095] Referring to FIG. 1, the manufacturing method (S1) may include a step (S11) of mixing a powdered binder with water to produce a liquid mixed binder.

[0096] Here, referring to FIG. 2, the powdered binder is a material in the form of a powder with calcium (CaO), magnesium (MgO), silicon (SiO2), and aluminum (Al2O3) as its main components, such as cement, blast furnace slag, fly ash, desulfurization gypsum, paper sludge incineration ash, anhydrous gypsum, and ferronickel slag. When mixed with water and measured, it exhibits alkalinity with a hydrogen ion concentration (pH) of 9 to 12. It combines with carbon dioxide to undergo a carbonation reaction to form calcium carbonate (CaCO3) or magnesium carbonate (MgCO3), and after being mixed with the original ground soil along with water, it strengthens the mixed soil through pozzolanic reaction, ettringite reaction, metasulfate reaction, etc.

[0097] In addition, the carbonation reaction is more active as the water / binder ratio increases, the hydrogen ion concentration (pH) increases, and the amount of Ca and Mg increases.

[0098] Here, the powdered binder can be mixed with 20 to 30 wt% cement, 35 to 55 wt% blast furnace slag, 5 to 10 wt% desulfurization gypsum, and 10 to 20 wt% fly ash.

[0099] The main material of the deep mixing treatment method presented in the specifications is slag cement, which requires about 50% cement, but the present invention can reduce the amount of cement used by more than half to 25% or less and expand the utilization of industrial by-products to reduce the amount of carbon dioxide generated by cement production. As industrial by-products, fly ash may include ash generated during the combustion or calcination process, such as high-calcium fly ash, Grade C fly ash, Grade F fly ash, coal ash, and paper sludge incineration ash.

[0100] In addition, the mixed water may be a mixed water to which a reactive admixture capable of simultaneously performing alkali activation and carbon dioxide adsorption functions has been added to the powdered binder.

[0101] For example, mixed water can be tap water, fresh water, seawater, purified water, rainwater, etc.

[0102] In addition, the mixing water may be water for mixing with the powdered binder, or water mixed with an admixture.

[0103] At this time, the reactive admixture may include at least one of potassium hydroxide (KOH), monoethyleneamine (MEA), sodium hydroxide (NaOH), and zeolite.

[0104] In addition, the mixed water in step S11 may be a mixed water to which a fluidity admixture containing at least one of an AE agent, a water reducer, a dispersant, and a fluidizing agent has been added.

[0105] Additionally, the amount of water mixed may be partially reduced by the fluidity admixture. The fluidity of the liquid mixed binder may be necessary for the flow rate when passing through the carbonation reaction device (100). The fluidity of the carbonation binder may be necessary to reduce the burden on the conveying device when conveying the carbonation binder and to increase the conveying distance. The fluidity of the carbonation mixture may be necessary to reduce the burden on the stirring device (123) described later when mixed with the original ground soil and to reduce the amount of water mixed to increase the strength of the soft ground improvement.

[0106] In addition, in step S11, the mixed water may be carbon dioxide bubble water or carbonated water.

[0107] Carbon dioxide bubble water refers to water in which carbon dioxide is dissolved in the form of microbubbles or nanobubbles. Since carbon dioxide is stored within the microbubbles, it can induce a carbon dioxide reaction over an extended period as it passes through a reaction device and the carbonation binder is transported. However, if there are too many bubbles, the strength of the soft ground improvement material may be reduced due to pores, so control is necessary. Additionally, carbonated water is a state in which carbon dioxide is dissolved in water. Carbon dioxide bubble water is CO2 inside the bubbles, while carbonated water is H2CO3.

[0108] In step S11, the liquid mixed binder has a fineness of 2,000 cm², taking into account the flow in the continuous flow method of step S12 to be described later. 2 It can be produced to include a powdered binder with a glycerin content of 1 / g (Blaine) or higher, and a mixed water having a weight ratio of water to the powdered binder of 70% or more and 120% or less. Specifically, the fineness is 2,500 cm⁻¹. 2It may be desirable to have a density of 2,500 cm² / g (Blaine) or higher. In other words, the liquid mixed binder may be provided with a powdered binder having a fineness of 2,500 cm² / g (Blaine) or higher and a mixed water with a weight ratio of 70% or more and 120% or less of water to the powdered binder, so that a certain level of flow rate can be achieved.

[0109] Fineness is an indicator representing the degree of fineness of a powder, and the specific surface area measured by the Blaine air permeability method is primarily used. Specific surface area is expressed as the surface area of ​​the powder per unit mass; the larger the specific surface area measured by the Blaine air permeability method, the finer the particles and the higher the fineness. Generally, binders (such as cement) with a larger Blaine specific surface area exhibit higher and faster reactivity.

[0110] Furthermore, the fineness must exceed a certain level to exhibit sufficient flow velocity when dissolved in water. Large and heterogeneous particles, such as sand or aggregates, tend to separate or fail to achieve sufficient flow velocity in the liquid binder state.

[0111] In addition, to reduce the use of cement, which can worsen the atmospheric environment due to high carbon dioxide emissions during the manufacture of liquid mixed binders, it is desirable to utilize industrial by-products such as blast furnace slag, fly ash, and desulfurization gypsum as much as possible.

[0112] In addition, in step S11, the mixed water may be fresh water (fresh water, tap water, etc.) or seawater (saltwater, seawater, etc.) depending on the water supply and work location. In this invention, the term "mixed water" refers to a liquid mixed with a powdered binder. It may also include a liquid mixed with various elements that can contribute to a synergistic effect in the manufacture of the target product, such as improving fluidity, controlling viscosity, controlling pH, and improving CO2 adsorption and reactivity.

[0113] In addition, in step S11, the liquid mixed binder refers to a binder state in which a powdered binder and a mixed water are mixed to exhibit liquid characteristics. Here, liquid characteristics refer to a state that has a flow level above a certain threshold, rather than a clumped state. Additionally, it may refer to a liquid in which solids are dispersed as a mixed suspension of various insoluble substances and liquids.

[0114] Referring to FIG. 1 and FIG. 5, 7 to 12 to be described later, the manufacturing method (S1) may include a step (S12) of producing a carbonated binder by reacting a liquid mixed binder produced by a carbonation reaction device (100) with carbon dioxide.

[0115] In other words, step S12 may be a step of producing a carbonated binder by reacting a liquid mixed binder with CO2 by a carbonation reaction device (100).

[0116] In the S12 step, the carbon dioxide reaction can be classified into direct carbonation and indirect carbonation depending on whether pretreatment is performed. Compared to the indirect carbonation method, where the reaction takes place after pretreatment—such as leaching alkaline earth metal ions from the raw material or dissolving CO2 in water in the form of bubbles—the direct carbonation method, which involves injecting carbon dioxide directly into the object to be carbonated to initiate the reaction, is advantageous in terms of both economics and efficiency.

[0117] Direct carbonation methods are classified into gas-solid direct carbonation and wet direct carbonation methods. Direct carbonation of gaseous carbon dioxide and solid binder powder has the disadvantage of a very slow conversion reaction, whereas the wet direct carbonation method, which involves reacting calcium and magnesium in the form of oxides or hydroxides of a liquid mixed binder (a mixture of powdered binder and water) with carbon dioxide, has a very fast and stable conversion rate.

[0118] [Chemical Formula 1] to [Chemical Formula 7] below are examples of chemical formulas in which calcium and magnesium undergo a carbonation reaction with carbon dioxide. As a result, carbonates (CaCO3, MgCO3) are converted into heat of reaction.

[0119] [Chemical Formula 1]

[0120]

[0121] [Chemical Formula 2]

[0122]

[0123] [Chemical Formula 3]

[0124]

[0125] [Chemical Formula 4]

[0126]

[0127] [Chemical Formula 5]

[0128]

[0129] [Chemical Formula 6]

[0130]

[0131] [Chemical Formula 7]

[0132]

[0133] [Chemical Formula 1] in the above chemical formula is explained as follows: when CaO reacts with CO2 to be converted into CaCO3, 1 mole of CO2 is consumed and 178 kJ of heat is generated. The 178 kJ / mol-CO2 shown in the reaction equation represents the amount of heat generated per mole of CO2, and this is information that explains the thermodynamic properties of the chemical reaction.

[0134] Figure 3a is a photograph of a carbon dioxide reaction experiment using a PET bottle conducted at this institution, and Figure 3b is a photograph of a phenolphthalein color change conducted at this institution.

[0135] In addition, referring to Fig. 3a, the present invention can confirm through a simple experiment that the reaction between the liquid mixed binder and carbon dioxide gas is very rapid. When a 750 ml PET bottle is filled with about one-third liquid mixed binder and the remaining two-thirds space is filled with carbon dioxide and shaken, it can be observed that the PET bottle immediately collapses due to the vacuum, leaving only the space occupied by the liquid mixed binder. When carbon dioxide is injected back into the collapsed PET bottle to restore it to its original state using injection pressure and the shaking process is repeated, the same reaction is observed more than 10 times. This is because the liquid mixed binder undergoes a carbonation reaction, converting into a solid carbonate, and the space occupied by the carbon dioxide immediately becomes a vacuum. At this time, when the temperature of the PET bottle is measured, the temperature rose from 28°C to 42°C during the process of conversion from the liquid mixed binder to the carbonation binder. From this, it was determined that the reaction rate of wet direct carbonation is fast and that an exothermic reaction occurs in parallel.

[0136] Additionally, referring to Fig. 3b, when a phenolphthalein solution is sprayed onto a sample of a DCM mixture consisting of a powdered binder, mixed water, and soil, it turns purple. This is because the pH of the DCM mixture is 10 or higher, making it a strong base. Phenolphthalein solution is an indicator that is colorless in acidic and neutral conditions but turns purple in basic conditions with a pH of 8.2 or higher. Furthermore, carbon dioxide is heavier than air and flows downward. After placing the sample, which has turned purple after spraying phenolphthalein, into a cup, if carbon dioxide is poured from another cup into the cup containing the sample, the purple color on the surface of the sample disappears immediately upon contact with the carbon dioxide. From this, it can be understood that the carbonation reaction occurs simply through contact with carbon dioxide, and the reaction rate is also very fast. If the sample is inverted, the purple color inside remains, but if carbon dioxide is brought into contact again, the purple color disappears immediately.

[0137] In conclusion, the carbonation reaction rate is very fast, and since the reaction occurs simply by contacting carbon dioxide and is limited to the contact surface, the carbonation reaction is more effective when the specific surface area of ​​the sample is maximized. In other words, the reaction contact surface with carbon dioxide must be maximized.

[0138] Therefore, the technical goal of the present invention is to construct a carbonation reaction device (100) that can maximize the reaction contact surface according to the results of the experiment.

[0139] According to the experimental results described above, in step S12, a liquid carbon dioxide storage tank, a vaporizer, and a pressure reducing device are connected to the carbonation reaction device (100) so that gaseous carbon dioxide can be injected.

[0140] In other words, in step S12, the carbonation reaction device (100) can be connected to a liquid carbon dioxide (LCO2) storage tank, a vaporizer, and a pressure reducing device (GSU; Gas Supply Unit, Gas Pressure Reducing Equipment) so that gaseous carbon dioxide can be injected.

[0141] Specifically, for the efficiency of carbon dioxide transport and storage, it must be liquid carbon dioxide. The vaporizer and pressure reducing device may be integrated. Various commercial technologies exist for vaporizers, such as the electric hot water type, which vaporizes liquid carbon dioxide by exchanging heat as it passes through a hot water tank containing the liquid carbon dioxide, and the atmospheric type, which vaporizes liquid carbon dioxide inside aluminum fin tubes by exchanging heat through external natural convection. A pressure reducing device may be required to adjust the pressure of the gaseous carbon dioxide discharged from the vaporizer.

[0142] In addition, carbon dioxide can exist in solid and liquid states depending on temperature and pressure. Based on the observation that the carbonation reaction is faster when there is a large surface area of ​​contact with the liquid mixed binder, the specific surface area of ​​carbon dioxide in solid or liquid states becomes very small; therefore, the reaction rate is inevitably significantly slower compared to the gaseous state where the specific surface area is maximized. Therefore, for a fast and stable continuous flow carbonation reaction, it is desirable to inject it into the carbonation reaction device (100) in a gaseous state. The specific gravity of liquid carbon dioxide is 1.031, and 1 L of liquid carbon dioxide is equivalent to 521 L of gaseous carbon dioxide. That is, since the specific surface area of ​​liquid carbon dioxide is about 500 times smaller than that of gaseous carbon dioxide, the carbonation rate is inevitably greatly affected, although it may vary depending on the pressure and temperature of the vaporization environment.

[0143] Only when it is gaseous carbon dioxide can the reaction rate be fast, and only when the reaction rate is fast can the carbonation reaction device (100) be implemented in a continuous flow manner.

[0144] At this time, the pressure reducing device includes a carbon dioxide buffer storage tank for buffering and storing the reduced-pressure gaseous carbon dioxide, and the carbon dioxide buffer storage tank may be equipped to maintain a pressure within a preset pressure range.

[0145] At this time, referring to FIGS. 5, 7 to 12 to be described later, the carbonation reaction device (100) may be provided to follow a continuous flow method in which a liquid mixed binder is introduced, reacts with carbon dioxide, and is discharged sequentially. In other words, the carbonation reaction device (100) may be a continuous flow method.

[0146] Here, the term "continuous flow method" may refer to a method in which a liquid binder is continuously introduced into a carbonation reaction device in a constant amount, an equivalent level of flow reaction takes place inside the carbonation reaction device (100), and the carbonation binder is converted into an equivalent amount and continuously discharged.

[0147] For example, for deep mixing processes that require a stable mass supply of materials, a continuous flow carbonation reaction device capable of continuously manufacturing carbonation binders by a constant flow rate must be provided.

[0148] Furthermore, since the civil engineering sector requires a large workforce and large specialized equipment, shortening the construction period and reducing waiting and maintenance times is a critical factor in terms of construction costs. To shorten the construction period, materials must be supplied in accordance with the efficiency of the construction equipment. Supplying materials via a continuous flow method rather than a batch method is the best way to increase construction equipment efficiency by utilizing the equipment continuously. In the case of a batch method, waiting times may occur. Since deep mixing processing equipment such as DCM is expensive and large-scale equipment, the production and supply of carbonation binders must proceed continuously and stably to maximize equipment efficiency, thereby minimizing construction costs and time.

[0149] In addition, according to the aforementioned experimental results, the carbonation reaction device in step S12 can be provided in a continuous flow manner. Specifically, according to the aforementioned experimental results, the wet direct carbonation method, in which a liquid mixed binder is reacted directly with carbon dioxide, is fast and stable. Furthermore, the carbonation reaction is more active when the pH is higher, the content of Ca and Mg is higher, and the water-to-binder ratio is higher; as a result of the carbonation reaction, carbonates (CaCO3, MgCO3, etc.), vacuum phenomena, and exothermic phenomena appear. Moreover, the reaction occurs simply by bringing the liquid mixed binder into contact with carbon dioxide. The greater the reaction contact surface area, the greater the amount of carbon dioxide reaction.

[0150] In other words, the continuous flow method means that manufacturing (production) is completed through a serial flow of input, reaction, and discharge, and that the flow is continuous and a constant amount is manufactured continuously. To process using the continuous flow method, the reaction time must be fast and the flowability must be good. To achieve a fast reaction time, it is advantageous to have a high hydrogen ion concentration (PH), a high content of Ca and Mg, and a high water-to-binder ratio. Therefore, since this manufacturing method applies a wet direct carbonation method that uses a powdered binder with a high PH and a high content of Ca and Mg, and a liquid mixed binder with a high water-to-binder ratio and good flowability, it is possible to process using the continuous flow method.

[0151] In addition, the manufacturing method (S1) may use gaseous carbon dioxide with a fast reaction rate to be provided in a continuous flow manner of the carbonation reaction device (100).

[0152] In addition, in order to configure a carbonation reaction device in a continuous flow manner by considering a gaseous carbon dioxide space that must be at least 14 times larger than the volume of the liquid mixed binder at 1 atmosphere, it is first possible to make only the liquid mixed binder the carbonation target, and the shape, type, efficiency, area, length, etc. of the carbonation reaction device (100) can be set by considering the flow rate (V), liquid level (A), flow rate (Q), viscosity, etc. of the liquid mixed binder, etc., and the reaction amount and space of the gaseous carbon dioxide, injection pressure, injection time, etc.

[0153] In addition, through experiments, the present institute confirmed the carbon dioxide reaction characteristics that allow setting the input amount, flow rate, droplet, and flow rate of the liquid mixed binder.

[0154] Figure 4 is a schematic diagram of the carbon dioxide reaction amount measurement test using a balloon conducted at this institution.

[0155] Specifically, the amount of carbon dioxide reaction can be inferred through a simple experiment using a balloon inflated with carbon dioxide as shown in Fig. 4, which is the amount of carbon dioxide reaction by wet direct carbonation. From this, the volume and weight of the amount of carbon dioxide reaction, which are proportional to the amount of liquid mixed binder, can be calculated.

[0156] To prepare a 1,165g DCM sample, 147g of powdered binder and 118g of mixed water are mixed to prepare 265g (22%) of liquid mixed binder. At this time, Type 2 slag cement is used as the powdered binder, and the volume of the liquid mixed binder is 181L. A flexible tube is inserted through the lid of a plastic bottle containing the liquid mixed binder and secured, and a balloon inflated with carbon dioxide is connected to the other end of the tube. The entire assembly is placed in water to confirm that it is in a sealed state.

[0157] In addition, carbon dioxide was blocked from flowing into the plastic bottle through a flexible tube by pressing it with clips, and the size of the balloon was measured to have an average diameter of 25 cm and a temperature of 26°C inside the plastic bottle. (At this time, the carbonation reaction occurring on the surface of the liquid mixed binder inside the plastic bottle was ignored as a conservative measure, and the pressure inside the balloon was assumed to be 1 atmosphere (atm).)

[0158] After that, the liquid mixed binder in the plastic bottle is shaken to increase the reaction contact surface area, and the clamp blocking the carbon dioxide flow is released. At this time, it was confirmed that after 2 to 3 seconds, the temperature of the plastic bottle becomes 39°C and the average diameter of the balloon decreases to 22 cm.

[0159] It was confirmed through calculation that the reduced volume of the balloon is 2,600 mL. When calculating the volume of 1 kg of carbon dioxide at 26°C and 1 atm, the molar mass of CO2 is 44 g / mol. Therefore, calculating the number of moles of 1 kg of CO2 gives 1,000 g / (44 g / mol) = 22.7272 mol. Also, from PV = nRT, V = nRT / P, so the volume of CO2 V = {22.7272 x 0.082 x (273 + 26)} / 1 = 557.225 L. Thus, it was confirmed that the volume of 1 kg of CO2 is 0.557 m³ and the weight of 1 m³ of CO2 is 1.79 kg.

[0160] In addition, when calculating the reaction amount of carbon dioxide, 147g of the powdered binder is converted to 63mL in volume, 118g of the mixed water is converted to 118mL in volume, and the liquid mixed binder is converted to 181mL in volume, and the reaction amount of carbon dioxide 0.0026m3 is converted to 4.65g in weight. Summarizing this, it is as shown in Equation 1 below.

[0161] [Equation 1]

[0162]

[0163] Through this, if 250 kg of powdered binder is added per 1 m³ of DCM mixture, 7.9 kg (= 250 kg x 3.16%) of carbon dioxide can be reacted. In addition, it was confirmed that a carbon dioxide space of at least 14.36 times the volume of the liquid mixed binder is required to induce the maximum reaction under 1 atmosphere.

[0164] Therefore, the reaction characteristics known from the experimental results can be important information for determining the size and resistance pressure of the carbonation reaction device (100), and for determining the amount of liquid mixed binder to be added, the flow rate, the drop, and the flow rate.

[0165] In addition, the carbonation reaction device (100) can be provided by carefully considering the instantaneous expansion pressure and heat exchange conditions caused by vaporization when some or all of the carbon dioxide is injected in a liquid state.

[0166] In addition, the carbonation reaction device (100) may be configured to minimize its volume by ensuring that gaseous carbon dioxide is continuously injected simultaneously with the reaction, and may be configured to resist temporary pressure fluctuations.

[0167] In addition, the carbonation reaction device (100) can be provided by considering the shape, method, area, length, etc., so that the reaction contact surface between the liquid mixed binder and carbon dioxide is maximized.

[0168] FIG. 5 is a drawing for explaining the case where the main body of a carbonation reaction device includes a static mixer section in the first aspect of the present invention, and FIG. 6 is a drawing for explaining the static mixer in the first aspect of the present invention.

[0169] FIG. 7 is a drawing for explaining the case where the main body of a carbonation reaction device includes a venturi tube section in the first aspect of the present invention.

[0170] FIG. 8a is a drawing for explaining a single venturi tube in the first aspect of the present invention, and FIG. 8b is a drawing for explaining a multi-venturi tube.

[0171] FIG. 9 is a drawing for explaining the case in which the main body of a carbonation reaction device includes a venturi tube section and a static mixer section in the first aspect of the present invention.

[0172] FIG. 10 is a drawing for explaining the case in which the main body of a carbonation reaction device includes a turbulent mixing section in the first aspect of the present invention.

[0173] Additionally, referring to FIGS. 5, 7, 9 and 10, the carbonation reaction device (100) may include an input section (110) into which a liquid mixed binder is introduced, a main body (120) that reacts with CO2 by maximizing the specific surface area of ​​the introduced liquid mixed binder, a discharge section (130) having a discharge port from which at least a portion of the reacted liquid mixed binder is discharged, and a carbon dioxide injection section (140) that injects carbon dioxide into the main body (120). Specifically, the carbonation reaction device (100) may each have one or more input sections (110) and discharge sections (130). Here, specific surface area refers to the surface area per unit mass, and the specific surface area is maximized as the contact surfaces between particles are separated by dispersing the particles of the liquid mixed binder, which are in contact and clumped together, into the smallest possible particles.

[0174] Additionally, the carbon dioxide injection unit (140) may be provided with one or more carbon dioxide injection ports and may include a transfer pipe for transporting carbon dioxide.

[0175] At this time, the input section (110) may include an input port (111) connected to the main body (120), a transfer pipe connected to the input port (111), and a pump (112) provided to apply pressure to inject the liquid mixed binder into the main body (120). In other words, the input section (110) may include a pump (112) and a transfer pipe. Additionally, a transfer pipe may be provided at the discharge port, and a pump (112) may be provided as needed.

[0176] Additionally, the pump (112) can be controlled so that the inlet (111) is closed by the liquid mixing binder into which it is introduced and the outlet is closed by the liquid mixing binder into which it is discharged, thereby allowing the interior of the main body (120) to be controlled to follow a continuous flow method while maintaining a closed state that is closed above a preset level of closure.

[0177] The inlet port (111) achieves a sealed state by continuously pushing a liquid mixed binder at a pressure higher than the internal pressure of the carbonation reaction device (100), and the outlet port achieves a sealed state by allowing the carbonation binder to be discharged while continuously resisting the internal pressure of the carbonation reaction device (100). By adjusting the input and discharge amounts to a constant level, the internal pressure and sealed state of the carbonation reaction device (100) can be continuously maintained. This can be achieved by installing a U-trap or buffer tank at the inlet port (111) and the outlet port, or by adjusting the transfer speed of the connected pump (112). Additionally, the pressure state and sealed state can be maintained by adjusting the cross-sectional area of ​​the inlet port (111) and the outlet port, taking into account the carbonation reaction speed and discharge speed according to the constant input speed.

[0178] Specifically, maintaining a stable and continuous sealed state is an important aspect of the carbonation reaction device (100). While it is obvious that it must be sealed to prevent carbon dioxide from diffusing into the air or being diluted with other gas components, there are many factors to consider when maintaining stable and continuous sealed conditions because the volume change of the gas with pressure is very large. This is especially true in a continuous flow method rather than a batch method. The sealed state must not be temporarily released while the inlet (111) and the outlet are being opened and closed. Furthermore, since mechanical devices such as screws or propellers that must be driven inside the sealed carbonation reaction device (100) require power to be transmitted from the outside to the inside, more effort is required to seal the area around the power shaft that operates through the sealed container. In the face of the contemporary challenge of reducing carbon dioxide in the atmosphere, a lot of energy has already been consumed in collecting carbon dioxide, and preventing carbon dioxide from being released back into the atmosphere is also an important reason why a sealed state must be maintained.

[0179] In addition, the amount of liquid mixed binder introduced into the carbonation reaction device (100) and the amount of carbonation binder discharged must be equal. Although the amount introduced and the amount discharged may fluctuate temporarily, the overall average amount over the operating time must be nearly the same. If the discharge amount is consistently greater than the amount introduced, the sealing state of the inlet (111) and the outlet may be released, and the amount of carbon dioxide reaction inside the carbonation reaction device (100) may decrease rapidly. At this time, if the outlet is temporarily blocked or the discharge amount is reduced to maintain sealing, the flow may be interrupted or stagnated. Conversely, if the amount introduced is consistently greater than the discharge amount, the liquid mixed binder inside the carbonation reaction device (100) becomes stagnant, causing an overload on the internal power device or affecting the flow and pressure. Therefore, only a continuous flow method can ensure stable sealing of the carbonation reaction device (100).

[0180] In other words, the inlet port (111) is closed (sealed) by a liquid mixing binder and the outlet port is closed (sealed) by a discharged carbonation binder, so that the pump (112) can be controlled to follow a continuous flow method while maintaining a closed state in which the interior of the main body (120) is closed above a preset level of closure.

[0181] Additionally, in step S12, due to the vacuum phenomenon caused by the carbonation reaction between the liquid mixed binder and carbon dioxide inside the main body (120), a negative pressure corresponding to at least a portion of the pressure required to inject carbon dioxide into the main body (120) may be formed in the carbon dioxide injection part (140).

[0182] For example, carbon dioxide can be sucked in through the carbon dioxide injection port (140) by negative pressure (vacuum) caused by a carbonation reaction. As another example, carbon dioxide can be sucked in through the carbon dioxide injection port by suction force due to the Venturi effect, and carbon dioxide can be injected through the carbon dioxide injection port by additional pressure.

[0183] Additionally, the carbonation reaction device (100) may be equipped with a pressure maintaining device that maintains the internal pressure of the carbonation reaction device (100) at a constant level. The pressure maintaining device may be equipped with a pressure measuring device that measures the internal pressure of the carbonation reaction device (100), a carbon dioxide pressurizing supply device that injects carbon dioxide, and a solenoid valve.

[0184] Specifically, the carbon dioxide space inside the carbonation reaction device (100) may need to be more than 10 times the volume of the liquid mixed binder. Therefore, it may be necessary to minimize the carbon dioxide space inside the carbonation reaction device (100).

[0185] Carbon dioxide is injected at a certain pressure so that it is faster than the rate at which the liquid mixed binder reacts with carbon dioxide inside the carbonation reaction device (100). The carbon dioxide must be injected by adjusting the pressure to a level that the carbonation reaction device (100) can accommodate.

[0186] Due to the negative pressure (vacuum) inside the reaction device caused by the carbonation reaction, carbon dioxide from the storage tank is drawn in to some extent through the carbon dioxide injection pipe, but the pressure may not be very high. Also, there is a possibility that the injection pipe may be temporarily blocked due to the liquid mixed binder. Therefore, continuously injecting carbon dioxide at a pressure higher than atmospheric pressure and faster than the vacuum generation rate of the carbonation reaction can serve to clear the blocked injection pipe, and a secondary effect can be obtained where the carbonation reaction is activated as the pressure increases. This allows the size of the carbonation reaction device (100) to be minimized and the effect of supplying only the amount of carbon dioxide required for the reaction to be obtained.

[0187] Additionally, the carbon dioxide pressurized supply device may be an air compressor, or the pressure reducing device or the buffer storage tank. It may be a method of supplying to the carbonation reaction device (100) using the magnetic pressure of the pressure reducing device or the buffer storage tank.

[0188] Additionally, for example, referring to FIGS. 5 and 6, the main body (120) may include a static mixer section (121) in the form of a static mixer, which includes a static mixer (121a) provided inside the passage to induce turbulent mixing for a liquid mixed binder that is discharged to a discharge section (130) connected to the other side, passing through a passage that is directly or indirectly connected to an input section (110) and a carbon dioxide injection section (140) on one side.

[0189] In other words, referring to FIG. 5, the carbonation reaction device (100) may include a pump (112) (transfer device), an input section (110) (transfer pipe and CO2 inlet), a static mixer (121a) (static mixer), and a discharge section (130) (including a transfer pipe).

[0190] Referring to FIG. 5, a pump (112) that moves at a constant amount and a constant speed may be installed on the side of the input section (110). At this time, the amount of carbon dioxide injected and the amount of the pump (112) transferred on the side of the input section (110) may be set to maintain a constant ratio.

[0191] Here, referring to FIGS. 5 and 6, the static mixer (121a) is a stirring (mixing) device that achieves continuous mixing by simply passing a fluid (liquid, gas, powder) through a pipe without any moving parts.

[0192] A static mixer (121a) is configured such that one or more mixing elements are arranged in succession inside a closed tube.

[0193] Continuous mixing is enabled by minimizing energy loss through turbulent mixing forces.

[0194] For example, referring to Fig. 6, the static mixer can be equipped as a helical mixer. The helical mixer is a typical shape of a static mixer. The elements are rectangular plates twisted 180 degrees, and are divided into left and right elements according to the direction of the twist and arranged continuously. Typically, the length of each element is based on a length of 1.5 times its diameter.

[0195] However, the shape of the static mixer (121a) is not limited to this, and static mixers of various shapes may be provided in the carbonation reaction device (100). Since this is obvious to a person skilled in the art, a more detailed explanation will be omitted.

[0196] At this time, referring to FIG. 6, if a static mixer (121a) is provided as a spiral mixer, the liquid mixing binder can be mixed based on the principles of splitting action, switching action, and inversion action.

[0197] Here, the splitting action refers to the phenomenon where, when a fluid passes through an element and is divided, the number of divisions increases exponentially with the number of elements. In this case, if S is the number of divisions and n is the number of elements, then S = 2n. If Di is the inner diameter of the pipe and d is the thickness of the fluid division (Thickness of section), then d = Di / 2n.

[0198] In addition, the switching action means that the fluid is sequentially exchanged from the center of the tube to the wall and from the wall to the center of the tube along the twist plane within the element.

[0199] In addition, the reversal action refers to the phenomenon where the fluid changes its direction of rotation for every element, undergoing a rapid reversal of inertial force to become turbulent stirring.

[0200] At this time, the static mixer (121a) minimizes resistance to fluid flow and can be applied to various fluid mixtures such as liquid and liquid, gas and gas, liquid and gas. In this invention, it is applied to the mixture of liquid and gas.

[0201] In addition, the static mixer can achieve superior mixing effects regardless of where it is installed during the process, and is equipped to prevent noise, vibration, or leakage during operation, thereby meeting the sealing conditions of the present invention.

[0202] In addition, compared to powered agitators, it has the advantage of requiring fewer breakdowns and maintenance, and does not require power for mixing.

[0203] Furthermore, the diversity of materials available for production allows for the mixing of any fluid. Process shortening, simplification, and continuity are possible, facilitating process management and resulting in significant benefits such as reduced production costs and energy savings.

[0204] As another example, referring to FIGS. 7 and FIGS. 8A, the main body (120) includes a venturi tube section (122) provided in the form of a venturi tube, the input section (110) is connected to one side of the venturi tube, the discharge section (130) is connected to the other side of the venturi tube, and the carbon dioxide injection section (140) may be provided so as to be located closer to the minimum cross-section position among the positions where the passage cross-section of the tube is at the maximum cross-section and the position where the minimum cross-section is at the venturi tube.

[0205] Referring to FIG. 5, the input section (110) may be equipped with a pump (112) that continuously transfers a constant amount at a constant speed. Additionally, as illustrated in the figure, the carbonation reaction device (100) may include a venturi tube equipped with a carbon dioxide injection section (140) (carbon dioxide intake port (including intake pipe)).

[0206] Specifically, carbon dioxide is sucked in by the Venturi tube while simultaneously being sprayed or mixed with liquid, thereby maximizing the reaction contact surface.

[0207] Here, a Venturi tube refers to a tube whose diameter gradually narrows and then expands. When a fluid flows regularly through a Venturi tube, the pressure is high and the fluid flow velocity is slow in the wide passages. Conversely, in the narrow passages, the fluid pressure is low and the flow velocity is fast. Furthermore, a carbon dioxide injection port located at a narrow passage self-absorbs carbon dioxide due to the high velocity and low pressure of the fluid, and the amount of carbon dioxide absorbed can be controlled by the fluid velocity. This is called the Venturi effect, and its hydraulic interpretation is known as Bernoulli's theorem.

[0208] Functionally, a Venturi tube can also be referred to as an ejector. The only difference is that a Venturi tube is equipped with a tube-shaped carbon dioxide inlet at a location where the passage is narrow, drawing in carbon dioxide by utilizing the characteristics of high flow velocity and low pressure; whereas an ejector draws in carbon dioxide by equipping the carbon dioxide inlet to surround the area where the flow velocity is high and the pressure is low using a high-pressure nozzle. In other words, while the Venturi tube and the ejector differ only in the shape of the carbon dioxide inlet, the principle of drawing in carbon dioxide by utilizing the difference in fluid velocity and pressure is the same, based on the Venturi effect.

[0209] In addition, there may be V-cones, flow nozzles, orifice plates, segmental wedges, etc., that perform functions similar to a Venturi tube. Here, except for the Venturi tube, cavities may form during fluid flow, causing flow resistance; therefore, the Venturi tube is most suitable for the continuous flow method of manufacturing a carbonation binder according to the present invention.

[0210] Additionally, referring to FIGS. 7 and FIGS. 8a, when a constant flow rate and a constant flow rate are continuously introduced and passed through the inlet (111), a constant amount of carbon dioxide is continuously sucked in through the inlet of the venturi tube. The liquid mixed binder and carbon dioxide sucked in at a constant ratio are sprayed as they pass rapidly through the narrow passage of the venturi tube, thereby maximizing the reaction contact surface. Accordingly, it is possible for the carbonation reaction rate to proceed rapidly.

[0211] Additionally, referring to FIG. 8a, the carbon dioxide injection port may be provided in the Venturi tube where the cross-section of the tube passage is closer to the position of the minimum cross-section between the position of the maximum cross-section and the position of the minimum cross-section. Since the positioning of the carbon dioxide injection port is obvious to a person skilled in the art, a more detailed explanation will be omitted.

[0212] Additionally, referring to FIG. 8b, the venturi tube section (122) may be provided as a multi-venturi tube as shown in FIG. 8b. In this case, the multi-venturi tube may refer to a single tube in which the carbon dioxide injection section (140) is one and the venturi tubes are configured in such a way that each venturi tube communicates with one carbon dioxide injection section (140).

[0213] At this time, the multi-venturi has a higher discharge pressure and vacuum suction rate compared to the single-venturi, and the discharge volume of the multi-venturi increases by 109% to 200% compared to the single-venturi, and the suction volume increases by 50% to 114% compared to the single-venturi.

[0214] As another example, referring to FIG. 9, the main body (120) may include a venturi tube section (122) which is configured in the form of a venturi tube with one side connected to an input section (110) and a carbon dioxide injection section (140) connected in the middle, and a static mixer (121a) section (121) which is configured in the form of a static mixer (121a) with one side connected to the other side of the venturi tube section (122) and the other side connected to a discharge section (130). Specifically, referring to FIG. 9, the static mixer section (121) configured in the form of a static mixer (121a) may be formed between the venturi tube section (122) and the discharge section (130).

[0215] In other words, referring to FIG. 9, one side of the venturi tube section (122) can be connected to the input section (110), and the other side of the venturi tube section (122) can be connected to the static mixer section (121).

[0216] Additionally, one side of the static mixer section (121) can be connected to the venturi tube section (122), and the other side of the static mixer section (121) can be connected to the discharge section (130).

[0217] In other words, referring to FIG. 9, the carbonation reaction device (100) may include an input section (110) (input port (111)), a venturi tube section (122) (venturi tube (including CO2 intake port / tube)), a static mixer section (121) (static mixer), and a discharge section (130) (discharge port). However, since the description of the venturi tube section (122) and the static mixer section (121) has been described above, a more detailed description will be omitted.

[0218] As another example, referring to FIG. 10, the main body (120) may include a venturi tube section (122) which is configured in the form of a venturi tube, with one side connected to an input section (110) and a carbon dioxide injection section (140) connected in the middle; and a turbulent mixing section (124) in which one side is connected to the other side of the venturi tube section (122), the other side is connected to a discharge section (130), and a chamber for inducing turbulent mixing is formed in the middle.

[0219] Specifically, referring to FIG. 10, the other side of the venturi tube section (122) is connected to the input section (110), and a carbon dioxide injection section (140) can be connected in the middle of the venturi tube section.

[0220] Additionally, referring to FIG. 10, one side of the turbulent mixing section (124) may be connected to the Venturi tube section (122), and the other side of the turbulent mixing section (124) may be connected to the discharge section (130).

[0221] In other words, referring to FIG. 10, the carbonation reaction device (100) may include an input section (110) (input port (111)), a venturi tube section (122) (venturi tube (including CO2 intake port / tube)), a turbulent mixing section (124) (turbulent mixing chamber), and a discharge section (130) (discharge port).

[0222] Specifically, after primary mixing is performed in the Venturi tube section (122) (Venturi tube), secondary mixing is performed by connecting to the turbulent mixing section (124) (turbulent mixing chamber). In the turbulent mixing section (124) (turbulent mixing chamber), the diameter of the tube widens rapidly and then narrows again, allowing residual carbon dioxide bubbles and the liquid mixing binder to be mixed by turbulence (vortex). This can maximize the reaction contact surface.

[0223] FIG. 11 is a drawing illustrating the appearance of a stirring device provided on the main body of a carbonation reaction device in the first aspect of the present invention.

[0224] As another example, referring to FIG. 11, the main body (120) may include a stirring device (123) that stirs the liquid mixed binder, which is discharged to a discharge part (130) connected to the other side through a passage that is directly or indirectly connected to an input part (110) and a carbon dioxide injection part (140) on one side, at a high speed to increase the reaction contact surface with carbon dioxide.

[0225] Specifically, referring to FIG. 11, a pump (112) that transfers a certain amount may be installed in the input section (110) and the discharge section (130). In addition, the liquid mixed binder in reaction inside the main body (120) of the carbonation reaction device (100) controls the amount of liquid mixed binder input, the amount of carbonation binder discharge, and the carbon dioxide injection pressure so that the input port (111) and the discharge port are always locked.

[0226] In other words, referring to FIG. 11, a stirring device (123) that stirs at high speed to maximize the reaction contact surface between carbon dioxide and the liquid mixed binder may be provided inside the main body (120) of the carbonation reaction device (100).

[0227] At this time, the part through which the power shaft (123a) of the stirring device (123) passes through the main body (120) of the carbonation reaction device (100) may be provided with consideration to maintain a sealed state. The paddle of the stirring device (123) may be provided with a shape that facilitates scooping up the liquid mixing binder and dispersing it into the carbon dioxide space. In addition, the main body (120) of the carbonation reaction device (100) and the stirring device (123) may be provided vertically or at an angle, or in a V-shape.

[0228] In addition, the pump (112) pressure can be set so that the amount of liquid binder injected through the input section (110) to maintain closure and the amount of carbonated binder discharged through the discharge section (130) are equal.

[0229] In addition, it is preferable to set the uppermost level of the liquid mixed binder inside the main body (120) to be lower than the level of the carbon dioxide inlet (to prevent backflow into the inlet).

[0230] FIG. 12 is a drawing for explaining a case in which, in the first aspect of the present invention, a carbon dioxide recovery unit is provided at the top of the main body of a carbonation reaction device and a carbon dioxide injection unit is provided at the bottom of the main body.

[0231] As another example, referring to FIG. 12, a carbon dioxide recovery unit (220) for recovering carbon dioxide may be provided at the top of the main body (120), and a carbon dioxide injection unit (140) for injecting carbon dioxide may be provided at the bottom of the main body (120).

[0232] Specifically, referring to FIG. 12, the input section (110) and the discharge section (130) may be equipped with a pump (112) that transfers a certain amount.

[0233] Additionally, the liquid mixed binder being reacted inside the main body (120) of the reaction device controls the amount of liquid mixed binder being injected and the amount of carbonation binder being discharged and the internal pressure caused by carbon dioxide so that the inlet (111) and the outlet (120) are always locked. As shown in FIG. 12, the main body (120) of the carbonation reaction device (100) is provided with one or more carbon dioxide injection parts (110) at the bottom of the main body (120) of the carbonation reaction device (100) to continuously inject carbon dioxide bubbles at high pressure to maximize the reaction contact surface between carbon dioxide and the liquid mixed binder, and a recovery port that is returned to the carbon dioxide tank by the internal pressure may be provided at the top of the main body (120) of the carbonation reaction device (100).

[0234] Additionally, a nozzle for spraying carbon dioxide as microbubbles may be provided on the side of the main body (120) of the carbon dioxide injection unit (140) of the carbonation reaction device (100).

[0235] At this time, the carbon dioxide injection part (140) may be provided so that the liquid mixed binder does not flow back. In addition, the carbon dioxide recovery port may be provided so that it is not blocked by the liquid mixed binder.

[0236] The main body (120) of the carbonation reaction device (100) may include a power-driven stirring device (123).

[0237] Specifically, referring to FIG. 11 and FIG. 12, as shown in FIG. 11, a stirring device (123) is provided inside the main body (120), and as shown in FIG. 12, one or more carbon dioxide injection parts (110) that continuously inject carbon dioxide bubbles at high pressure to maximize the reaction contact surface between carbon dioxide and a liquid mixed binder are provided at the bottom of the main body (120) of the carbonation reaction device (100), and a recovery port that is returned to the carbon dioxide tank by internal pressure may be provided at the top of the main body (120) of the carbonation reaction device (100).

[0238] In addition, the recovered carbon dioxide can be reused by connecting it to a storage tank connected to the carbon dioxide injection unit (140).

[0239] FIG. 13 is a drawing illustrating the case in which a liquid mixed binder is dispersed and introduced into a carbon dioxide environment in the first aspect of the present invention.

[0240] In addition, referring to FIG. 13 as another example, a pump (112) that transfers a certain amount may be provided in the input section (110) and the discharge section (130), and as shown in FIG. 13, the carbonation mixing binder inside the main body (120) of the carbonation reaction device (100) can control the input amount of the liquid mixing binder, the dispersion amount of the liquid mixing binder dispersion device (150), the discharge amount of the carbonation binder, and the internal pressure caused by carbon dioxide so that the discharge section (130) (discharge port) is always locked.

[0241] Additionally, as illustrated in FIG. 13, the main body (120) of the carbonation reaction device has an input section (110) configured at the top of the main body (120) of the carbonation reaction device (100) for continuously dispersing and injecting by a liquid mixed binder dispersion device (150) to maximize the reaction contact surface between carbon dioxide and the liquid mixed binder, and a carbon dioxide injection section (140) configured in the carbonation reaction device (100) for injecting carbon dioxide so that the inside of the carbonation reaction device (100) is always filled with carbon dioxide, and the lower part of the main body (120) of the carbonation reaction device (100) is configured in a form in which the carbonation binder (10) collects downward by gravity, and a discharge section (130) may be provided in the part where the carbonation binder (10) is accumulated in the lower part of the main body (120) of the carbonation reaction device (100).

[0242] At this time, the amount of liquid mixed binder to be injected can be set with consideration so that the liquid mixed binder does not flow back through the carbon dioxide injection part (140).

[0243] Additionally, referring to FIGS. 7, 8a and 9, a power-driven stirring device (123) may be provided inside the main body (120) of the carbonation reaction device (100), and the aforementioned Venturi tube may be used as a liquid mixing binder dispersion device (150).

[0244] FIG. 14 is a drawing for explaining a carbon dioxide recovery device in the first aspect of the present invention.

[0245] Referring to FIG. 14, the discharge section (130) of the carbonation reaction device (100) is connected to a carbon dioxide recovery device (200), and the carbon dioxide recovery device (200) may include a carbon dioxide separation chamber (210) that is connected to the discharge section (130) and extends downward, and a carbon dioxide recovery section (220) connected to the upper side of the carbon dioxide separation chamber (210).

[0246] Specifically, a carbon dioxide recovery device (200) (CO2 Degas Separator) may be connected after the discharge section (130) of the carbonation reaction device (100). The carbon dioxide recovery device (200) is composed of a carbon dioxide separation chamber (210) and a carbon dioxide recovery section (220) (recovery port (pipe)). The carbon dioxide separation chamber (210) may be provided as a sealed chamber connected to the discharge section and extending downward (vertically downward), and the carbon dioxide recovery section (220) (recovery port (pipe)) may be provided at the top of the carbon dioxide separation chamber (210).

[0247] Additionally, a relief valve may be connected to the carbon dioxide recovery section (220) (recovery port (pipe)) as needed. A back pressure valve or a general valve may be connected to the lower part of the carbon dioxide separation chamber (210) as needed.

[0248] Additionally, the carbon dioxide recovery device (200) (CO2 Degas Separator) can be configured so that the carbonation binder can be collected downward by gravity, and the light unreacted carbon dioxide can be collected upward and discharged to the carbon dioxide recovery unit (220).

[0249] Additionally, the carbon dioxide recovery unit (220) can be recycled by being connected to a carbon dioxide storage tank for injecting carbon dioxide into the carbonation reaction device (100).

[0250] In addition, a vibration device can be attached to the carbon dioxide separation chamber (210) to facilitate the separation of unreacted carbon dioxide from the carbonation binder.

[0251] Specifically, even if a certain amount of unreacted carbon dioxide is contained in the carbonation mixture (carbonate binder + original ground soil), it can react slowly during the curing period and the unreacted carbon dioxide can be permanently stored in the ground. However, since too much unreacted carbon dioxide remains as voids in the soft ground improvement after curing is complete and may hinder strength development, the amount of unreacted carbon dioxide can be controlled by adjusting the intensity of the vibration device.

[0252] In other words, the carbon dioxide recovery device (200) may include a vibration device that applies vibration to the carbon dioxide separation chamber (210). The vibration device may be provided to facilitate the separation of unreacted carbon dioxide mixed with the discharged carbonation binder.

[0253] Additionally, the carbonation reaction device (100) may be provided such that a plurality of unit carbonation reaction devices (100) are arranged in series, a plurality of unit carbonation reaction devices (100) are arranged in parallel, or a plurality of unit carbonation reaction devices (100) are arranged in a matrix form that combines series and parallel.

[0254] The carbonation reaction device (100) may be configured such that two or more are arranged in series, or two or more are arranged in parallel, or the carbonation reaction device (100) may be configured as a matrix arranged in series and parallel. Additionally, the matrix may be provided in multiple layers to reduce the space occupied by the device.

[0255] Additionally, the carbonation reaction device (100) may include a booster pump system installed in the connection portion between interconnected unit carbonation reaction devices (100).

[0256] In other words, in a carbonation reaction device (100) composed of multiple unit carbonation reaction devices (100) arranged in series, parallel, or matrix, one or more booster pump systems (112) can be provided between the unit carbonation reaction devices (100). Booster pumps can be installed as needed at intervals to control the flow rate of each unit carbonation reaction device (100). Through this, the input and output amounts can be controlled consistently.

[0257] Here, the term "booster" in technical terms implies "to add power," "to increase," or "to amplify," and can refer to the amplification of flow energy resulting from pressure loss. Additionally, a booster pump is also referred to as a pressurization pump station. A booster pump is defined as a device installed in the middle of a circulation system or in the middle of a transport system to increase lost pressure. A booster pump system may be equipped with a control device (control panel) and pressure, temperature, and flow sensors.

[0258] FIG. 15a is a drawing for explaining the overall length of a carbonation reaction apparatus in the first aspect of the present invention, FIG. 15b is a drawing for explaining another embodiment in which a pipe diameter design is made considering the gradient of vacuum phenomenon progression in the first aspect of the present invention, and FIG. 15c is a drawing for explaining a plurality of unit devices in the first aspect of the present invention.

[0259] Additionally, referring to FIG. 15a, the total length of the carbonation reaction device (100) can be set to have a difference in flow rate so that a continuous fluid flow is maintained with friction in the state where the carbon dioxide reaction proceeds beyond a preset reaction amount, taking into account the vacuum phenomenon that occurs during the reaction of carbon dioxide.

[0260] The total length of the carbonation reaction device (100) can be set to have a flow rate greater than the flow rate required for the carbonation reaction device (100). Here, referring to (b) of FIG. 15a, when friction is ignored, the required flow rate of the carbonation reaction device (100) is such that if the input flow rate is V1 and the output flow rate is V3, then since A1 and A3 are the same, V1 and V3 must also be mutually identical (the difference in flow rates between them is 0) so that continuous fluid flow can be maintained.

[0261] More specifically, referring to FIG. 15a, as the liquid mixed binder passes through the static mixer section (121), it is converted into a carbonation binder, and the distribution of carbon dioxide in the flow cross-section (flow drop) is eliminated. At this time, when friction in the pipe is ignored, Q (flow rate) = A (flow drop) x V (flow velocity). Since the flow rate (QL) is constant and the flow drop (A1) of the liquid mixed binder and the flow drop (A3) of the carbonation binder are identical, the flow velocity (V1) of the liquid mixed binder and the flow velocity (V3) of the carbonation binder are identical.

[0262] When carbon dioxide is injected, the liquid-mixed binder droplet (A2) shrinks by the amount of the droplet (AG) occupied by the carbon dioxide, causing the flow velocity (V2) to increase, thereby maintaining a constant flow rate (QL). As the carbon dioxide undergoes a carbonation reaction, the liquid-mixed binder droplet (A2) gradually expands due to the vacuum phenomenon, and the process proceeds to a state where the flow velocity (V2) slows down.

[0263] As such, ideally, when friction is ignored, it can be understood that V2 becomes faster than V1 and V3 as shown above, resulting in a faster flow in the middle. However, in practice, if friction is considered (friction with physical components, friction at the solid-gas interface), the order may be V1 > V2 > V3.

[0264] As another example, referring to FIG. 15b, the flow cross-section of the liquid mixed binder is constant, and the cross-section after carbon dioxide injection is expanded to account for the cross-sectional area occupied by carbon dioxide, and then gradually reduced to the original cross-sectional area of ​​the tube to account for the vacuum phenomenon caused by the carbonation reaction. The static mixer inside the tube can change according to the change in the cross-sectional area of ​​the tube.

[0265] In other words, ideally, the length of the carbonation reaction device (100) is set to be longer than the length at which the carbon dioxide reaction is completed and the flow rate is restored, and it would be desirable to set it so that the flow rate at the inlet of the carbonation reaction device (100) is maintained at the same level at the outlet, but in practice, since friction must be taken into account, the length of the unit reaction device (100) can be set to have a flow rate difference that maintains a continuous fluid flow while taking friction into account.

[0266] Additionally, referring to FIG. 15c, the carbonation reaction device (100) includes a plurality of unit reaction devices (100a) connected in series, and each unit device (100a) includes a carbon dioxide injection unit (140) and a static mixer (121a), and the length of each unit reaction device (100a) can be set to have a flow rate difference such that a continuous fluid flow is maintained with respect to friction when the carbon dioxide reaction proceeds beyond a preset reaction amount.

[0267] Specifically, referring to FIG. 15c, the carbonation reaction device (100) may be connected in series with a unit reaction device (100a) equipped with a carbon dioxide injection unit (140) and a static mixer (121a). At this time, it is preferable to determine and proceed with the setting that allows for the maintenance of a continuous flow after an initial setting (test) is performed according to the specifications (inner diameter) of the device, the characteristics of the binder material, and various actual application items.

[0268] Additionally, the length of each unit reaction device (100a) is ideally set to be longer than the length at which the carbon dioxide reaction is completed and the flow rate is restored, and it is desirable to set it so that the flow rate at the inlet of the unit reaction device (100a) is maintained at the same level at the outlet, but in practice, considering friction, it can be set to have a difference in flow rate that maintains a continuous fluid flow.

[0269] In addition, with reference to FIGS. 7, FIGS. 8a, FIGS. 8b and FIGS. 9, the length of the carbonation reaction device (100) equipped with a Venturi tube section (122) can also be set so that the flow rate and velocity change due to the carbonation reaction and vacuum phenomenon as described above, thereby maintaining a constant flow rate.

[0270] Specifically, in order for the carbon dioxide and liquid mixed binder to be mixed smoothly by the splitting, switching, and inversion actions of the static mixer (122a) in the flow cross-sectional area, the proportion that carbon dioxide can occupy is less than 50%. This is because the high-density material must be at least 50% or more to have the required flow rate, and the static mixer (122a) must operate smoothly only when it is above a certain level. In other words, the cross-sectional area ratio of carbon dioxide to the liquid mixed binder is approximately 100% (1:1) at maximum, and considering the mixing flow rate as constant, the maximum volume (flow rate) ratio of carbon dioxide to the liquid mixed binder is also approximately 1:1.

[0271] The amount of carbon dioxide required for the carbonation binder must be at least 5 times the volume of the liquid mixed binder to be effective, and in the experiment, 14 times the volume of carbon dioxide was required.

[0272] In addition, the flow cross-sectional area (flow volume) of the mixed fluid (CO2, liquid mixed binder) must completely fill the cross-sectional area of ​​the static mixer pipe, and during the process of becoming a carbonation binder, gaseous carbon dioxide solidifies and the space it occupied becomes a vacuum.

[0273] At this time, the static mixer and the venturi tube can perform mixing and suction functions only when there is a flow rate above a certain level.

[0274] In addition, to maintain the flow velocity, carbon dioxide must be injected while taking into account the flow cross-sectional area that changes due to the carbonation vacuum phenomenon.

[0275] In addition, since at least five times the volume of carbon dioxide must be injected compared to the volume of the liquid mixed binder, it must be possible to inject carbon dioxide multiple times at each point where the carbonation reaction is completed.

[0276] However, as described above, at the point where the carbonation reaction is completed, the space occupied by carbon dioxide is eliminated by a vacuum phenomenon, and the flow rate can be maintained by the flow of only the liquid mixed binder, so the mixing function of the static mixer can operate smoothly even if carbon dioxide is injected multiple times.

[0277] In other words, the carbonation reaction device (100) in the present invention may be provided with a length such that the flow rate is the same at the input section (110) and the discharge section (130) so that carbon dioxide injection can be continuously carried out at intervals.

[0278] In addition, the carbonation reaction device (100) in the present invention may be provided with unit reaction devices (100a) connected in series, and each unit reaction device (100a) may be provided with a carbon dioxide inlet (120) so that carbon dioxide can be injected intermittently, and each unit reaction device (100a) may be provided with a length such that the flow rate is equal at the input section (110) and the discharge section (130), so that even if they are continuously connected in series, the input and output flow rates remain constant, thereby reducing (preventing) the load on the continuous flow or the occurrence of gaps.

[0279] When manufacturing a carbonation binder using the aforementioned manufacturing method, carbonation can be contributed to carbon neutrality by utilizing captured carbon dioxide.

[0280] In addition, storing captured carbon dioxide can contribute to carbon neutrality.

[0281] In addition, reducing cement usage can contribute to carbon neutrality by suppressing carbon dioxide emissions.

[0282] Furthermore, by utilizing carbon dioxide to increase the strength of soft ground improvements, the amount of binder used is reduced. This leads to lower transportation and storage costs, reduces carbon dioxide emissions during transportation, reduces carbon dioxide emissions during cement production, and allows for the acquisition of carbon credits, thereby enhancing economic and environmental benefits in various aspects.

[0283] <Method for manufacturing a carbonation binder according to the second aspect of the present invention>

[0284] Hereinafter, a method for manufacturing a carbonation binder according to the second aspect of the present invention will be described. However, since the method for manufacturing a carbonation binder according to the second aspect of the present invention shares the same or corresponding technical features as the method for manufacturing a carbonation binder according to the first aspect of the present invention, redundant descriptions regarding configurations identical or similar to those of the method for manufacturing a carbonation binder according to the first aspect of the present invention will be brief or omitted.

[0285] However, below, the method for manufacturing a carbonation binder according to the second aspect of the present invention will be described based on FIGS. 1 to 4 (for reference, FIGS. 1 to 4 are drawings applicable to both the first and second aspects of the present invention) and FIGS. 16 to 30 (drawings corresponding to the method for manufacturing a carbonation binder according to the second aspect of the present invention). For reference, the method for manufacturing a carbonation binder according to the first aspect of the present invention described above was described based on FIGS. 1 to 4 (for reference, FIGS. 1 to 4 are drawings applicable to both the first and second aspects of the present invention) and FIGS. 5 to 15 (drawings corresponding to the method for manufacturing a carbonation binder according to the first aspect of the present invention).

[0286] In particular, regarding the reference numerals, even if they are identical to the reference numerals used in the method for manufacturing a carbonation binder according to the first aspect of the present invention, they may refer to different configurations, and in such cases, the reference numerals may be understood to refer to the configuration indicated by FIGS. 16 to 30. For example, in the case of reference numeral 121, in the method for manufacturing a carbonation binder according to the first aspect of the present invention, it may be understood as a reference numeral referring to the static mixer section (121) when referring to FIG. 5, etc., but in the method for manufacturing a carbonation binder according to the second aspect of the present invention described below, it may be understood as a reference numeral referring to the reaction section (121) when referring to FIG. 16, etc.

[0287] Referring to FIG. 1, a method for manufacturing a carbonated binder according to the second aspect of the present invention (hereinafter referred to as the ‘method for manufacturing (S1)’) may include a step (S11) of mixing a powdered binder with water to produce a liquid mixed binder.

[0288] However, since the description of the powdered binder has been previously described in the description of the first aspect of the present invention, a more detailed description will be omitted.

[0289] The main material of the deep mixing treatment method presented in the specifications is slag cement, which requires about 30% to 50% cement; however, the present invention can reduce the amount of cement used by about half to around 15% to 25% and expand the utilization of industrial by-products, thereby reducing the amount of carbon dioxide generated by cement production. Fly ash may include ash generated during the combustion or calcination process of high-calcium fly ash, Grade C fly ash, Grade F fly ash, coal ash, paper sludge incineration ash, etc.

[0290] In addition, the mixed water may be a mixed water to which a reactive admixture capable of simultaneously performing alkali activation and carbon dioxide adsorption functions has been added to the powdered binder.

[0291] For example, mixed water can be tap water, fresh water, seawater, purified water, rainwater, etc.

[0292] In addition, the mixing water may be water for mixing with the powdered binder, or water mixed with an admixture.

[0293] At this time, the reactive admixture may include at least one of potassium hydroxide (KOH), monoethyleneamine (MEA), sodium hydroxide (NaOH), and zeolite.

[0294] In addition, at step S11, the mixed water may be a mixed water to which a fluidity admixture containing at least one of an AE agent, a water reducer, an AE water reducer, a high-performance AE water reducer, a high-performance water reducer, and a fluidizing agent has been added.

[0295] Additionally, the amount of mixing water may be partially reduced by the fluidity admixture. The fluidity of the liquid mixing binder may be necessary for the flow rate when passing through the circulation conveyor (12) of the carbonation reaction device (1) described later. The fluidity of the carbonation binder may be necessary to reduce the load on the conveyor when conveying the carbonation binder and to increase the conveying distance. The fluidity of the carbonation mixture may be necessary to increase the strength of the soft ground improvement by reducing the load on the stirring device when mixed with the original ground soil and reducing the amount of mixing water.

[0296] In addition, in step S11, the mixed water may be carbon dioxide bubble water or carbonated water.

[0297] However, since the description of carbon dioxide bubble water and carbonated water has been previously described in the description of the first aspect of the present invention, a more detailed description will be omitted.

[0298] In step S11, the liquid mixed binder can be produced by considering the flow rate in the circulating flow method of step S12 described later, and including a powdered binder with a fineness of 2,000 cm2 / g (Blaine) or more and a pH of 10 or more, and a mixed water with a weight ratio of 50% or more to the powdered binder.

[0299] Fineness is an indicator representing the degree of fineness of a powder, and the specific surface area measured by the Blaine air permeability method is primarily used. Specific surface area is expressed as the surface area of ​​the powder per unit mass; the larger the specific surface area measured by the Blaine air permeability method, the finer the particles and the higher the fineness. Generally, binders (such as cement) with a larger Blaine specific surface area exhibit higher and faster reactivity.

[0300] In addition, the fineness must reach a certain level (for example, the fineness may be 3,000 blein, but is not limited to this) to exhibit sufficient flow velocity when dissolved in water. Large and heterogeneous particles, such as sand or aggregate, tend to separate or fail to achieve sufficient flow velocity in the liquid-phase mixed binder state.

[0301] In addition, to reduce the use of cement, which can worsen the atmospheric environment due to high carbon dioxide emissions during the manufacture of liquid mixed binders, it is desirable to utilize industrial by-products such as blast furnace slag, fly ash, and desulfurization gypsum as much as possible.

[0302] In addition, in step S11, the mixed water may be fresh water (fresh water, tap water, etc.) or seawater (saltwater, seawater, etc.) depending on the water supply and work location. In this invention, the term "mixed water" refers to a liquid mixed with a powdered binder. It may also include a liquid mixed with various elements that can contribute to a synergistic effect in the manufacture of the target product, such as improving fluidity, controlling viscosity, controlling pH, and improving CO2 adsorption and reactivity.

[0303] In addition, in step S11, the liquid mixed binder refers to a binder state in which the powdered binder and the mixed water are mixed to exhibit liquid characteristics. Here, liquid characteristics refer to a state that has a flow level above a certain threshold rather than a clumped state. Furthermore, the liquid mixed binder can also be referred to as a slurry. Here, a slurry can refer to muddy water that is highly fluid due to a large amount of water mixed with soil, or a liquid in which solids are dispersed as a mixed suspension of various insoluble substances and liquids.

[0304] FIG. 16 is a drawing for explaining step S12 in the second aspect of the present invention.

[0305] Additionally, referring to FIG. 1 and FIG. 16, the manufacturing method (S1) may include a step (S12) of producing a carbonated binder by reacting a liquid mixed binder produced by a carbonation reaction device (1) with carbon dioxide.

[0306] At this time, the carbonation reaction device (1) can be provided by carefully considering the instantaneous expansion pressure and heat exchange conditions due to vaporization when part or all of the carbon dioxide is injected in a liquid state.

[0307] In addition, the carbonation reaction device (1) may be configured to allow gaseous carbon dioxide to be continuously injected simultaneously with the reaction in order to minimize the volume of the carbonation reaction device (1), and may be configured to resist temporary pressure fluctuations.

[0308] In addition, the carbonation reaction device (1) can be provided by considering the shape, method, area, length, etc., so that the reaction contact surface between the liquid mixed binder and carbon dioxide is maximized.

[0309] Specifically, referring to FIG. 16, the carbonation reaction device (1) may include a binder chamber (11) comprising a second input section (111) into which the generated liquid mixed binder is introduced and a second discharge section (112) for discharging at least some of the reacted liquid mixed binder.

[0310] Referring to FIG. 16, the binder chamber (11) may include a chamber body (113) connected to a second input section (111) into which the generated liquid mixed binder is introduced, a second discharge section (112) into which the carbonation binder is discharged, and a circulation transfer device (12) to be described later. At this time, the carbonation binder may be manufactured when the carbonation reaction is completed. Here, the completion of the carbonation reaction does not mean only that the carbonation reaction of the liquid mixed binder is 100% completed, but the carbonation reaction may be considered completed when a predetermined standard is reached, such as when the carbonation reaction of the liquid mixed binder is carried out for more than a preset time, or when the liquid mixed binder passes through the reaction section to be described later more than a preset number of times and reacts for more than a preset amount of reaction, or when the amount of temperature change due to the reaction heat during the carbonation reaction of the liquid mixed binder is greater than a preset amount of temperature change. For example, if it is expected that exceeding a preset standard will cause the carbonation reaction gradient to become extremely gentle and significantly reduce reaction efficiency, the carbonation reaction may be considered complete upon reaching that preset standard.

[0311] Additionally, referring to FIG. 16, the second discharge unit (112) may be provided at the bottom of the binder chamber (11).

[0312] Additionally, referring to FIG. 16, the second input section (111) may be equipped with an input valve (111a) capable of controlling the amount of liquid mixed binder to be input. For example, the input valve (111a) may be provided as a proportional control valve or a controllable on / off (open / close valve).

[0313] Additionally, referring to FIG. 16, the second discharge unit (112) may be equipped with a discharge valve (112a) capable of controlling the amount of carbonated binder produced by completing the carbonation reaction of the liquid mixed binder. For example, the discharge valve (112a) may be provided as a proportional control valve or a controllable on / off (open / close valve).

[0314] Additionally, the binder chamber (11) (specifically the chamber body (113)) may be a box-shaped chamber with a square cross section, the binder chamber (11) may be a circular pipe with the same diameter as the transfer pipe (123) of the circulating transfer device (12) described later, and the binder chamber (11) may be a T-shaped composite chamber equipped with a transfer pipe (123) connected vertically downward to an upper horizontal cylindrical chamber.

[0315] Additionally, referring to FIG. 16, the carbonation reaction device (1) may include a circulation transfer device (12) connected to a binder chamber (11) and including a reaction section (121) in which the introduced liquid mixed binder reacts with carbon dioxide.

[0316] At this time, referring to FIG. 16 and FIG. 17, 19, 22, 26, and 29 to be described later, in step S12, a carbonated binder can be manufactured by reacting a liquid mixed binder, which is introduced by a pump (122a) and a reaction unit (121) to be described later, with carbon dioxide while passing through a circulation transfer device (12).

[0317] In other words, step S12 may be a step of producing a carbonation binder by reacting the liquid mixed binder with CO2 by passing it through a circulation transfer device (12) that includes a pump (122a) (specifically, a venturi pump (122a)) and a reaction unit (121) to be described later.

[0318] In step S12, the carbon dioxide reaction can be classified into direct carbonation and indirect carbonation depending on whether pretreatment is performed.

[0319] In addition, direct carbonation methods are classified into gas-solid direct carbonation and wet direct carbonation methods. Direct carbonation of gaseous carbon dioxide and solid binder powder has the disadvantage of a very slow conversion reaction, whereas the wet direct carbonation method, in which calcium and magnesium in the form of oxides or hydroxides of a liquid mixed binder (a mixture of powdered binder and water) are reacted with carbon dioxide, has a very fast and stable conversion rate.

[0320] However, since the explanation regarding direct carbonation and indirect carbonation has been described above in the description of the first aspect of the present invention, a more detailed explanation will be omitted.

[0321] In addition, since the wet direct carbonation method of reacting calcium and magnesium in the form of oxides or hydroxides of a liquid mixed binder, which is a mixture of a powdered binder and mixed water, with carbon dioxide has a very fast and stable conversion rate, as previously mentioned in the description of the first aspect of the present invention with reference to [Chemical Formula 1] to [Chemical Formula 7] and FIG. 3a and FIG. 3b, a more detailed explanation will be omitted.

[0322] In conclusion, the carbonation reaction rate is very fast, and since the reaction occurs simply by contacting carbon dioxide and is limited to the contact surface, the carbonation reaction is more effective when the specific surface area of ​​the sample is maximized. In other words, the carbon reaction contact surface must be maximized.

[0323] Therefore, the technical objective of the present invention is to construct a carbonation reaction device (1) that can maximize the reaction contact surface according to the results of the experiment.

[0324] Additionally, referring to FIG. 16, carbon dioxide can be supplied to the reaction unit (121) by a carbon dioxide injection unit (15) connected to a circulation transfer device (12). Specifically, according to the experimental results described above, in step S12, gaseous carbon dioxide can be injected by connecting a liquid carbon dioxide storage tank, a vaporizer (13), and a pressure reduction device to the circulation transfer device (12).

[0325] In other words, referring to FIG. 16, in step S12, the carbonation reaction device (1) can be connected to a liquid carbon dioxide (LCO2) storage tank, a vaporizer (13), and a pressure reducing device (GSU; Gas Supply Unit, Gas Pressure Reducing Equipment) so that gaseous carbon dioxide can be supplied.

[0326] Specifically, for efficient transport and storage of carbon dioxide, it must be liquid carbon dioxide. The vaporizer (13) and the pressure reducing device may be integrated. There are various commercial technologies for the vaporizer (13), such as an electric hot water type that vaporizes liquid carbon dioxide by exchanging heat while passing it through a hot water tank where it is stored, and an atmospheric type that vaporizes liquid carbon dioxide inside an aluminum fin tube by exchanging heat through external natural convection. A pressure reducing device may be required to adjust the pressure of the gaseous carbon dioxide discharged from the vaporizer (13).

[0327] In addition, carbon dioxide can exist in solid and liquid states depending on temperature and pressure. Based on the observation that the carbonation reaction is faster when there is a large surface area of ​​contact with the liquid mixed binder, the specific surface area of ​​carbon dioxide in solid or liquid states becomes very small; therefore, the reaction rate is inevitably significantly slower compared to the gaseous state where the specific surface area is maximized. Thus, for a fast and stable continuous flow carbonation reaction, it is desirable to supply it to the carbonation reaction device (1) in a gaseous state. The specific gravity of liquid carbon dioxide is 1.031, and 1 L of liquid carbon dioxide is equivalent to 521 L of gaseous carbon dioxide. In other words, since the specific surface area of ​​liquid carbon dioxide is about 500 times smaller than that of gaseous carbon dioxide, the carbonation rate is inevitably greatly affected, although it may vary depending on the pressure and temperature of the vaporization environment.

[0328] In other words, it is possible to implement a carbonation reaction device (1) by means of a reaction unit (121) (tubular mixing device) that operates by a fast flow rate only when the reaction rate is fast and only when the reaction rate is fast.

[0329] At this time, the pressure reduction device includes a carbon dioxide buffer storage tank (14) that buffers and stores the reduced pressure gaseous carbon dioxide, and the carbon dioxide buffer storage tank (14) may be configured to maintain a pressure within a preset pressure range.

[0330] In addition, the present invention confirmed the carbon dioxide reaction characteristics that allow setting the transfer amount, flow rate, droplet, and flow rate of the liquid mixed binder through experiments, as illustrated in the aforementioned Figure 4.

[0331] However, since the explanation of the experiment illustrated in Fig. 4 has already been described with reference to [Equation 1] in the explanation of the first aspect of the present invention, a more detailed explanation will be omitted.

[0332] Therefore, the reaction characteristics known from the experimental results can be important information for determining the size, number of cycles, and time of the carbonation reaction device (1), and for determining the flow rate, drop, and flow rate of the liquid mixed binder.

[0333] The important details regarding the manufacturing method (S1) based on the aforementioned experimental results are summarized as follows.

[0334] A wet direct carbonation method is a fast, stable, and effective method for manufacturing carbonation binders by mixing a powdered binder rich in Mg and Ca and high pH with water to produce it, and then reacting it with carbon dioxide.

[0335] In addition, since the liquid mixed binder reacts very rapidly at the contact surface with gaseous carbon dioxide, maximizing the reaction contact surface is most necessary to carbonate a large amount of the liquid mixed binder.

[0336] In addition, it can be seen that due to the carbonation reaction, gaseous carbon dioxide is converted into solid calcium carbonate or magnesium carbonate, the temperature rises due to the heat of the reaction, and the space occupied by gaseous carbon dioxide becomes a vacuum.

[0337] In addition, the amount of carbon dioxide required to make the carbonation binder may be about 14 times the volume of the liquid mixed binder.

[0338] Accordingly, as described above, the carbonation reaction device (1) can be provided by carefully considering the instantaneous expansion pressure and heat exchange conditions due to vaporization when some or all of the carbon dioxide is injected in a liquid state.

[0339] In addition, the carbonation reaction device (1) may be configured to allow gaseous carbon dioxide to be continuously injected simultaneously with the reaction in order to minimize the volume of the carbonation reaction device (1), and may be configured to resist temporary pressure fluctuations.

[0340] In addition, the carbonation reaction device (1) can be provided by considering the shape, method, area, length, etc., so that the reaction contact surface between the liquid mixed binder and carbon dioxide is maximized.

[0341] Additionally, referring to FIG. 16, the circulating transfer device (12) may include a reaction section (121), an inlet section (122) connected to the binder chamber (11) through which a liquid mixed binder is introduced from the binder chamber (11), and a transfer pipe (123) provided to allow the liquid mixed binder introduced into the inlet section (122) to move toward the reaction section (121). Here, the reaction section (121) may include a third input section (1211) connected to the transfer pipe (123) and into which the liquid mixed binder that has moved along the transfer pipe (123) is introduced, a main body (1212) in which the introduced liquid mixed binder reacts with carbon dioxide, and a third discharge section (1213) in which at least a portion of the reacted liquid mixed binder is discharged to the binder chamber (11).

[0342] Referring to FIG. 16, as described above, the binder carbonation reaction device (1) can be provided to follow a circulation flow method in which a liquid mixed binder is introduced into a circulation transfer device (12) through an inlet (122) connected to a chamber, the liquid mixed binder introduced into the inlet (122) moves along a transfer pipe (123) and is introduced into a reaction unit (121) through a third input unit (1211), and then, after the liquid mixed binder reacts with at least some gaseous carbon dioxide in the reaction unit (121), is discharged through a third discharge unit (1213) and placed back into the binder chamber (11), so that the liquid mixed binder passes through the reaction unit (121) repeatedly. For reference, although it was explained that the discharge is discharged through the third discharge section (1213) and then returned to the binder chamber (11), a discharge section (not shown in the drawing) corresponding to the inlet section (122) may be provided separately from the third discharge section (1213), and such a discharge section and the third discharge section (1213) may be interconnected. In other words, when viewed as a whole of the circulation transfer device (12), an inlet section (122) and a discharge section (not shown in the drawing) are provided, and a reaction section having a third input section and a third discharge section may be located between such an inlet section (122) and a discharge section. In this case, the third discharge section of the reaction section may also serve as the discharge section of the circulation transfer device (12), and the discharge section of the circulation transfer device (12) may be omitted.

[0343] Additionally, referring to FIGS. 16, 17 and FIGS. 19 to 28 to be described later, the reaction section (121) (tubular mixing device) may refer to a device that inhales carbon dioxide due to a pressure difference and sprays it, or mixes it through actions such as physical division, conversion, or inversion, when a liquid mixing binder filling the main body (1212) (inside the tube) flows at a high flow rate. A Venturi tube and a static mixer (12121a) to be described later may be provided as representative tubular mixing devices. An advantage of the reaction section (121) is that no other power source is required for mixing, except for the fluid flow inside the tube.

[0344] In addition, the characteristic of the reaction unit (121) (tubular mixing device) is that it is a device capable of achieving a mixing function that maximizes the reaction contact surface only when the mixed fluid containing carbon dioxide and a liquid mixed binder has a flow rate of at least a certain level. In other words, the reaction unit (121) (tubular mixing device) requires a flow rate of at least a certain level because it utilizes the pressure difference generated by the flow rate or performs physical operations such as splitting, switching, and inversion based on the flow rate. Accordingly, in order to secure a flow rate of at least a certain level, the reaction unit (121) needs to be formed in a tubular shape, and it is preferable that it be provided in the form of a circular tube.

[0345] In addition, since the amount of carbon dioxide (flow cross-sectional area) occupied by the carbon dioxide in the mixed fluid passing through the reaction section (121) (tubular mixing device) is inevitably equal to or smaller than the amount of carbon dioxide occupied by the liquid mixed binder, in order to react about 14 times the volume of carbon dioxide as in the experiment above, it must be a method of circulation that passes through the reaction section (121) (tubular mixing device) repeatedly.

[0346] In other words, to process in a circulating manner, the reaction time must be fast and the flowability must be good. To achieve a fast reaction time, it is advantageous to have a high hydrogen ion concentration (PH), a high amount of Ca and Mg components, and a high water-to-binder ratio. Therefore, the present manufacturing method (S1) can be processed in a circulating manner because it applies a wet direct carbonation method using a powdered binder with a high PH and a high amount of Ca and Mg components, and a liquid mixed binder with a high water-to-binder ratio and good flowability.

[0347] In addition, the manufacturing method (S1) may use gaseous carbon dioxide with a fast reaction rate to be provided in a circulating manner of the carbonation reaction device (1).

[0348] In addition, in order to configure the carbonation reaction device (1) in a circulating manner by considering the gaseous carbon dioxide space, which must be at least 14 times larger than the volume of the liquid mixed binder at 1 atmosphere, it is first possible to make only the liquid mixed binder the carbonation target, and by considering the flow rate (V), liquid level (A), flow rate (Q), viscosity, etc. of the liquid mixed binder, etc., and the reaction amount and space of the gaseous carbon dioxide, injection pressure, injection time, etc., the shape, type, efficiency, area, length, etc. of the carbonation reaction device (1) can be set, and the number of repetitions and circulation time passing through the reaction section (121) (tubular mixing device) can be determined.

[0349] FIG. 17 is a drawing for explaining a binder chamber configured to allow a liquid mixed binder to flow spirally in the second aspect of the present invention or in the seventh aspect to be described later, and FIG. 18 is a cross-sectional view AA of FIG. 17.

[0350] Specifically, FIG. 17 is a conceptual diagram for explaining a circulating carbonation reaction device (1) that applies a cyclone chamber in which a liquid mixed binder can flow spirally, and FIG. 18 is a conceptual diagram for explaining the shape of the outflow cross-section and the direction of outflow of the top (AA cross-section) of the cyclone chamber.

[0351] Additionally, referring to FIGS. 17 and 18, the third discharge section (1213) is connected so that the liquid mixed binder discharged therefrom forms a spiral flow that proceeds spirally along the direction of gravity within the binder chamber (11), and the inlet section (122) can be connected to the binder chamber (11) below the third discharge section (1213) to implement a circulating flow method.

[0352] Specifically, referring to FIGS. 17 and 18, the binder chamber (11) is provided in a cone shape with a diameter that decreases as it goes downward, and the third discharge part (1213) can be connected to the inside of the binder chamber (11) so that a liquid mixed binder that has reacted with carbon dioxide at least partially is discharged in the circumferential direction of the binder chamber (11) or in the tangential direction thereof.

[0353] For example, referring to FIG. 17, the binder chamber (11) (specifically the chamber body (113)) of the carbonation reaction device (1) may be in the form of a cyclone. The upper part of the binder chamber (11) may be in the form of a cylinder, and the lower part may be in the form of a cone with a gradually decreasing diameter. Here, the upper part may refer to the side where the third discharge part (1213) is connected to the binder chamber (11), and the lower part may refer to the side where the inlet part (122) is connected to the binder chamber (11). In other words, the inlet part (122) of the circulation transfer device (12) is connected to the lower side of the binder chamber (11), and the third discharge part (1213) is connected to the upper side of the binder chamber (11), so that the circulation flow of the circulation transfer device (12) can flow from bottom to top.

[0354] Additionally, referring to FIG. 18, the third discharge section (1213) of the circulating transfer device (12) can be connected to flow out (discharge) in the circumferential direction of the chamber body (113) so that rotation occurs at the top of the binder chamber (11). Accordingly, a spiral flow that proceeds spirally along the direction of gravity can be formed within the binder chamber (11).

[0355] As a result, the high-density liquid moves outward due to centrifugal force, and the relatively lighter gas (CO2) moves inward. Additionally, the high-density liquid moves downward due to gravity, and the relatively lighter gas (CO2) moves upward, causing a spiral flow to occur inside the chamber body (113), which has the advantage of separating unreacted carbon dioxide from the liquid binder and allowing it to be circulated.

[0356] The formation of a fluid flow in a downward spiral direction acts to allow the liquid mixed binder to flow more quickly into and out of the binder chamber (11) and the circulation transfer device (12). Additionally, the liquid mixed binder flow inside the chamber body (113) is created in the order required for the carbonation reaction according to the spiral flow, thereby providing the advantage of flowing into the inlet of the circulation transfer device (12).

[0357] Additionally, a spiral protruding guide that induces a spiral fluid flow may be attached to the inner surface of the chamber body (113) (cyclone binder chamber). Furthermore, the effect of the mixing action can be enhanced by a protruding attachment capable of splitting and reversing the fluid flow.

[0358] Specifically, even if a certain amount of unreacted carbon dioxide is contained in the carbonation mixture (carbonate binder + original ground soil), it can react slowly during the curing period, and the unreacted carbon dioxide can be permanently stored in the ground.

[0359] However, since too much unreacted carbon dioxide remains as voids in the soft ground improvement after curing is complete and may hinder strength development, the amount of residual carbon dioxide can be controlled by separating and recovering the unreacted carbon dioxide through a cyclone chamber in which the liquid mixed binder can flow spirally, as shown in FIGS. 17 and 18.

[0360] In addition, the upper surface of the binder chamber (11) is configured in a cone shape that slopes toward the center to collect unreacted carbon dioxide, and an unreacted carbon dioxide recovery pipe (16), which will be described later, is connected to the apex to form an efficient carbon dioxide recovery device.

[0361] In addition, the carbonation reaction device (1) may not be a method of introducing a liquid mixed binder into the second input section (111) of the carbonation reaction device (1), but may instead produce a liquid mixed binder inside the binder chamber (11) by directly introducing a powdered binder and mixed water into the binder chamber (11) and stirring with a separate stirring device. There may be an advantage in omitting a separate device for producing a liquid mixed binder.

[0362] Additionally, referring to FIG. 16, a carbon dioxide injection unit (15) that injects carbon dioxide directly or indirectly into a reaction unit (121) may be connected to the circulation transfer device (12).

[0363] For example, the carbon dioxide injection unit (15) can be directly connected to the reaction unit (121) as shown by the solid line in FIG. 16 to directly inject carbon dioxide into the reaction unit (121).

[0364] As another example, the carbon dioxide injection unit (15) can be connected to the pump (122a) described later, as shown by the dotted line in FIG. 16, to indirectly inject carbon dioxide into the reaction unit (121).

[0365] Specifically, at least one carbon dioxide injection part (15) (carbon dioxide injection pipe) may be connected to the circulation transfer device (12). The location where the carbon dioxide injection part (15) can be connected may be a pump (122a) among the components of the circulation transfer device (12), a reaction part (121) (tubular mixing device), and a transfer pipe (123) connecting them.

[0366] Additionally, in step S12, a negative pressure corresponding to at least a portion of the pressure required to supply carbon dioxide into the circulation transport device (12) can be formed in the carbon dioxide injection unit (15) through a carbonation reaction between the liquid mixed binder and carbon dioxide by the reaction unit (121) (tubular mixing device). For example, carbon dioxide can be sucked into the circulation transport device (12) through the carbon dioxide injection unit (15) by the negative pressure (vacuum) caused by the carbonation reaction.

[0367] Additionally, referring to FIGS. 16 and 17, a carbon dioxide recovery pipe (16) may be connected to the binder chamber (11) so that carbon dioxide that has not reacted with the liquid mixed binder among the carbon dioxide injected from the carbon dioxide injection unit (15) is recovered into the carbon dioxide buffer storage tank (14).

[0368] Specifically, a carbon dioxide recovery pipe (16) (connecting pipe) for recovering unreacted carbon dioxide may be provided at the top of the binder chamber (11) of the carbonation reaction device (1). The recovered unreacted carbon dioxide can be recycled by connecting it to a carbon dioxide storage tank. In the face of the contemporary challenge of reducing carbon dioxide in the atmosphere, a significant amount of energy has already been consumed in capturing and collecting carbon dioxide, and preventing carbon dioxide from being released back into the atmosphere is also an important reason for installing the carbon dioxide recovery pipe (16) (recovery device).

[0369] Additionally, the inlet section (122) may include an inlet connected to the binder chamber (11) and a pump (122a) provided to apply pressure to introduce the liquid mixed binder into the reaction section (121).

[0370] Specifically, a pump (122a) that transfers a liquid mixed binder at a preset amount and a preset speed may be installed at the inlet side (flow starting point) of the circulation transfer device (12). At this time, the transfer amount and carbon dioxide injection amount of the pump (122a) at the inlet side may be set to maintain a preset ratio.

[0371] At this time, the preset amount can be set by considering the amount of carbon dioxide that can react with the liquid mixed binder introduced into the reaction section (121), and the preset speed can be set by considering the reaction with the carbon dioxide that is injected by the liquid mixed binder introduced into the reaction section (121).

[0372] Additionally, the carbonation reaction device (1) may be provided to follow a circulating flow method that allows the liquid mixed binder to repeatedly pass through the reaction section (121).

[0373] Referring to FIG. 16, the circulation flow may refer to a flow in which the liquid mixed binder repeatedly reacts with carbon dioxide in the reaction section (121).

[0374] At this time, the liquid mixed binder reacts repeatedly with carbon dioxide, and a means to control the circulation time or the number of circulations may be required. The manufacturing of the carbonation binder must be completed in as short a time as possible, and the carbonation binder must be transferred to the second discharge unit (112). Due to the continuous circulation flow, it is difficult to directly count or verify the number of circulations. Therefore, as an indirect means of verifying the level of carbonation reaction of the liquid mixed binder, the completion of the carbonation binder manufacturing can be recognized and controlled by measuring the amount of temperature change due to the heat of reaction or by measuring the flow rate of injected carbon dioxide. A method for controlling the number of circulations will be described later.

[0375] Specifically, referring to FIG. 16, as described above, the circulation transfer device (12) may include an inlet section (122) (inlet), a pump (122a), a reaction section (121) (tubular mixing device), and a transfer pipe (123). In other words, the circulation transfer device (12) is a pipe connected to flow from bottom to top in a binder chamber (11) filled with a liquid mixed binder, and may be configured such that a pump (122a) is provided after the inlet section (122) (inlet) at the flow starting point, and at least one reaction section (121) (tubular mixing device) is included after the pump (122a) at the flow ending point. As another example, the circulation transfer device (12) may be connected to flow from top to bottom in a binder chamber (11) filled with a liquid mixed binder. When flowing from top to bottom, the liquid-mixed binder can benefit from the action of gravity, and conversely, when flowing from bottom to top, the gaseous carbon dioxide can benefit from the action of buoyancy.

[0376] The pump (122a) of the circulation transfer device (12) creates a circulation flow that introduces a liquid mixed binder into the inlet (122) connected to the lower part of the binder chamber (11) by pumping operation, and discharges the binder that has undergone a carbonation reaction into the third discharge part (1213) (outlet) connected to the upper part of the binder chamber (11) so that it is contained back into the binder chamber (11).

[0377] And, when passing through the reaction section (121) (tubular mixing device) included in the circulation transfer device (12), the carbon dioxide sucked in or injected into the circulation transfer device (12) causes a carbonation reaction with the liquid mixing binder, and the carbonation reaction can be repeated by the circulation flow.

[0378] FIGS. 19 and 20 are drawings for explaining the case where the reaction section of a carbonation reaction device includes a static mixer section in the second aspect of the present invention or the seventh aspect to be described later, and FIG. 21 is a drawing for explaining the static mixer in the second aspect of the present invention or the seventh aspect to be described later.

[0379] Additionally, referring to FIGS. 19 to 21, the main body (1212) may include a static mixer section (12121) that includes a static mixer (12121a) provided inside the passage to induce turbulent mixing for a liquid mixed binder that is discharged to a third discharge section (1213) connected to the other side, passing through a passage that is directly or indirectly connected to a third input section (1211) and a carbon dioxide injection section (15) on one side.

[0380] Specifically, referring to FIGS. 19 and 20, the reaction section (121) of the circulating transfer device (12) may include a third input section (1211) (transfer pipe (123) inlet section (122)), a carbon dioxide injection section (15) (CO2 inlet), a static mixer section (12121) including a static mixer (12121a) (Static Mixer), and a third discharge section (1213) (transfer pipe (123) outlet section).

[0381] Here, referring to FIGS. 20 and 21, the static mixer (12121a) is a mixing (stirring) device that achieves continuous mixing by simply passing a fluid (liquid, gas, powder) through a pipe without any moving parts.

[0382] A static mixer (12121a) is configured such that one or more mixing elements are arranged in succession inside a closed tube.

[0383] In addition, the static mixer (12121a) enables continuous mixing by minimizing energy loss through turbulent mixing force.

[0384] For example, referring to FIGS. 20 and 21, the static mixer (12121a) may be equipped as a helical mixer. The helical mixer is a typical shape of the static mixer (12121a). The elements are formed by twisting a rectangular plate 180 degrees, and are divided into left elements and right elements according to the direction of the twist and arranged continuously. Typically, the length of each element is based on a length of 1.5 times its diameter.

[0385] However, the shape of the static mixer (12121a) is not limited to this, and static mixers (12121a) of various shapes may be provided in the carbonation reaction device (1). Since this is obvious to a person skilled in the art, a more detailed explanation will be omitted.

[0386] At this time, referring to FIGS. 20 and 21, if a static mixer (12121a) is provided as a spiral mixer, the liquid mixing binder can be mixed based on the principles of splitting action, conversion action, and inversion action.

[0387] Here, the splitting action refers to the phenomenon where, when a fluid passes through an element and is divided, the number of divisions increases exponentially with the number of elements. In this case, if S is the number of divisions and n is the number of elements, then S = 2n. If Di is the inner diameter of the pipe and d is the thickness of the fluid division (Thickness of section), then d = Di / 2n.

[0388] In addition, the switching action means that the fluid is sequentially exchanged from the center of the tube to the wall and from the wall to the center of the tube along the twist plane within the element.

[0389] In addition, the reversal action refers to the phenomenon where the fluid changes its direction of rotation for every element, undergoing a rapid reversal of inertial force to become turbulent stirring.

[0390] At this time, the static mixer (12121a) minimizes resistance to fluid flow and can be applied to various fluid mixtures such as liquid and liquid, gas and gas, liquid and gas. In this invention, it is applied to the mixture of liquid and gas.

[0391] In addition, the static mixer (12121a) can achieve an excellent mixing effect regardless of where it is installed during the process, and is equipped so as not to produce noise, vibration, or leakage during operation, thus conforming to the circulation method of the present invention.

[0392] In addition, the static mixer (12121a) has the advantage of requiring less breakdown and maintenance compared to a power-type agitator, and does not require power for mixing.

[0393] In addition, the static mixer (12121a) can mix any fluid due to the variety of materials that can be manufactured. Since the process can be shortened, simplified, and continuous, process management is easy, and there are significant effects such as reduced production costs and energy savings.

[0394] FIGS. 22 and 23 are drawings for explaining the case where the reaction section of a carbonation reaction device includes a venturi tube section in the second aspect of the present invention or the seventh aspect to be described later, and FIG. 24 is a drawing for explaining the venturi tube section in the second aspect of the present invention or the seventh aspect to be described later.

[0395] Additionally, referring to FIGS. 22 to 24 as another example, the main body (1212) includes a venturi tube section (12122) provided in the form of a venturi tube, a third input section (1211) (liquid mixing binder inlet section (122)) is connected to one side of the venturi tube, a third discharge section (1213) (outlet section) is connected to the other side of the venturi tube, and a carbon dioxide injection section (15) may be provided so as to be located closer to the minimum cross-section position among the position where the passage cross-section of the tube is the maximum cross-section and the position where the minimum cross-section is the minimum cross-section in the venturi tube.

[0396] Specifically, referring to FIGS. 22 and 23, the reaction section (121) (tubular mixing device) may include a venturi tube section (12122) equipped with a carbon dioxide injection section (15) (carbon dioxide intake port (including intake tube)).

[0397] More specifically, carbon dioxide is sucked in by the venturi tube section while a liquid mixed binder is sprayed, thereby maximizing the reaction contact surface.

[0398] Here, a Venturi tube refers to a tube whose diameter gradually narrows and then expands. It is distinguished from an orifice, which refers to a tube that narrows rapidly. When a fluid flows regularly through a Venturi tube, the pressure is high and the fluid flow velocity is slow in the wider passages. Conversely, in the narrower passages, the fluid pressure is low and the flow velocity is fast. This is called the Venturi effect, and its hydraulic interpretation is known as Bernoulli's theorem.

[0399] A Venturi tube can also be functionally referred to as an ejector. The only difference is that a Venturi tube is equipped with a tube-shaped carbon dioxide injection port (15) (carbon dioxide inlet) at a location where the passage of the tube is narrow, thereby inhaling carbon dioxide by utilizing the characteristics of high flow velocity and low pressure, whereas an ejector is equipped with a carbon dioxide injection port (15) that surrounds the area where the flow velocity is high and the pressure is low by a high-pressure nozzle to inhale carbon dioxide. In other words, the Venturi tube and the ejector differ only in the shape of the carbon dioxide injection port (15), but the principle of inhaling carbon dioxide by utilizing the difference in fluid flow velocity and pressure is the same, based on the Venturi effect.

[0400] In addition, there may be V-cones, flow nozzles, orifice plates, segmental wedges, etc., that perform functions similar to a Venturi tube. Here, except for the Venturi tube, all of them may cause flow resistance due to the formation of cavities during fluid flow; therefore, the Venturi tube is most suitable for the continuous flow method of manufacturing a carbonation binder according to the present invention. The term "Venturi tube" in the present invention may include ejectors, injectors, V-cones, flow nozzles, orifice plates, and segmental wedges that utilize the Venturi effect.

[0401] Additionally, referring to FIGS. 23 and 24, when a constant flow rate and a constant flow rate are continuously introduced and passed through the third input section (1211), a constant amount of carbon dioxide is continuously sucked in through the carbon dioxide injection section (15) (carbon dioxide suction section (suction port)) of the venturi tube. As the liquid mixed binder and carbon dioxide introduced at a constant ratio pass rapidly through the narrow passage of the venturi tube and are sprayed, the reaction contact surface is maximized. Accordingly, it is possible for the carbonation reaction rate to proceed rapidly.

[0402] As another example, carbon dioxide can be sucked in by the suction force due to the Venturi effect through the carbon dioxide injection part (15) (carbon dioxide injection port), and carbon dioxide can be injected by additional pressure through the carbon dioxide injection part (15) (carbon dioxide injection port).

[0403] Additionally, referring to FIGS. 23 and 24, the carbon dioxide injection unit (15) may be provided in the venturi tube closer to the position of the minimum cross-section between the position of the maximum cross-section and the position of the minimum cross-section of the passage in the venturi tube. Since the positioning of the carbon dioxide injection unit (15) is obvious to a person skilled in the art, a more detailed explanation will be omitted.

[0404] FIG. 25 is a drawing for explaining a multi-venturi tube in the second aspect of the present invention or in the seventh aspect to be described later.

[0405] In addition, the single venturi tubes shown in FIGS. 23 and 24 can all be replaced with multi-venturi tubes as shown in FIG. 25.

[0406] Specifically, referring to FIGS. 23 and 24, a single venturi tube may be composed of one venturi tube and one carbon dioxide injection part (15) (carbon dioxide intake port (tube)) in one third input part (1211). On the other hand, referring to FIG. 25, a multi-venturi tube may be provided such that multiple venturi tubes are distributed across the cross-section of the tube for one third input part (1211) and share one carbon dioxide injection part (15) (carbon dioxide intake port (tube)).

[0407] At this time, the multi-venturi tube has the advantage of higher outflow pressure and vacuum suction rate compared to the single-venturi tube. The outflow volume of the multi-venturi tube increases by 109% to 200% and the suction volume increases by 50% to 114% compared to the single-venturi tube.

[0408] FIGS. 26 and 27 are drawings for explaining the case in which the reaction section of a carbonation reaction device includes a venturi tube section and a static mixer section in the second aspect of the present invention or the seventh aspect to be described later.

[0409] As another example, referring to FIGS. 26 and 27, the reaction section (121) of the circulation transfer device (12) may include a venturi tube section (12122) which is configured in the form of a venturi tube with one side connected to a third input section (1211) and a carbon dioxide injection section (15) connected in the middle, and a static mixer section (12121) which is configured in the form of a static mixer (12121a) with one side connected to the other side of the venturi tube section (12122) and connected to a third discharge section (1213) (outflow section) on the other side. For example, referring to FIG. 27, the static mixer section (12121) configured in the form of a static mixer (12121a) may be formed between the venturi tube section (12122) and the third discharge section (1213).

[0410] Specifically, referring to FIG. 27, one side of the venturi tube section (12122) can be connected to the third input section (1211), and the other side of the venturi tube section (12122) can be connected to the static mixer section (12121).

[0411] In other words, referring to FIG. 20, the reaction section (121) may include a third input section (1211), a venturi tube section (12122) (venturi tube (including CO2 intake port / tube)), a static mixer section (12121) (static mixer (12121a)), and a third discharge section (1213) (outlet). However, since the description of the venturi tube section (12122) and the static mixer section (12121) has been described above, a more detailed description will be omitted.

[0412] FIGS. 28 and 29 are drawings for explaining the case where the pump is equipped as a venturi pump in the second aspect of the present invention or in the seventh aspect to be described later.

[0413] Additionally, referring to FIGS. 28 and 29, the aforementioned pump (122a) may be a venturi pump (122a) provided to inject carbon dioxide at a pressure higher than a preset pressure and to apply pressure such that a liquid mixed binder is injected into the main body (1212) by the vacuum generated through the injection of carbon dioxide at a pressure higher than the preset pressure.

[0414] At this time, a preset pressure may be set to act as the pressure at which the liquid mixed binder is injected into the reaction section (121).

[0415] Referring to FIG. 28, the Venturi pump (122a) is a pump (122a) that creates a vacuum inside the tube by injecting high-pressure carbon dioxide into the center of the tube, sucks in the fluid, and then transports it by gas pressure. If the diameter of the tube at the location where high-pressure carbon dioxide is injected is narrowed, the Venturi effect can be obtained more significantly. Due to the Venturi effect, the flow velocity in the narrowed tube is sucked in and the pressure is lowered. Consequently, a vacuum is created inside the tube, allowing the liquid mixed binder to be sucked in. As the diameter of the tube gradually widens, the liquid mixed binder and gaseous CO2 are mixed to create a sprayed flow. The application of the Venturi pump (122a) can have the advantage of simultaneously solving carbon dioxide injection and circulation pumping with a single high-pressure compressor.

[0416] At this time, referring to FIG. 29, as described above, the carbon dioxide injection unit (15) is connected to a pump (122a) (specifically a venturi pump (122a)) to indirectly inject carbon dioxide into the reaction unit (121).

[0417] Additionally, with reference to FIGS. 16, 17, 19, 22, 26, and 29, the carbonation reaction device (1) includes a temperature measuring device (17) for measuring the temperature inside the binder chamber (11), and can control the number of times the liquid mixed binder repeatedly passes through the reaction section (121) based on the temperature measured by the temperature measuring device (17).

[0418] As described above, it is difficult to directly count or verify the number of cycles in the carbonation reaction device (1) due to the continuous circulation flow. Therefore, the carbonation reaction device (1) may include a temperature measuring device (17) for measuring the amount of temperature change due to reaction heat in order to verify the carbonation reaction level of the liquid mixed binder.

[0419] For example, the temperature inside the binder chamber (11) can be set when the liquid mixed binder reaches a preset reaction amount through testing or calculation. Additionally, when the temperature inside the binder chamber (11) reaches the preset temperature via the temperature measuring device (17), the carbonation reaction device (1) can be controlled so that the liquid mixed binder stops passing through the reaction section (121) and is discharged through the second discharge section (112). For example, if it is expected that the progress of the carbonation reaction will be significantly slowed down when the preset temperature is exceeded, discharge control to the second discharge section (112) can be performed when the preset temperature is reached.

[0420] Additionally, the temperature measuring device (17) may be equipped with various measuring devices capable of measuring the temperature of the binder chamber (11). Since this is obvious to a person skilled in the art, a more detailed explanation will be omitted.

[0421] Specifically, with reference to FIGS. 16, 17, 19, 22, 26, and 29, the binder chamber (11) of the carbonation reaction device (1) is equipped with a temperature measuring device (17) (binder temperature measuring device) capable of measuring the temperature inside the binder chamber (11) (specifically, the chamber body (113)). By monitoring the temperature change caused by the carbonation reaction and controlling the carbon dioxide supply amount and the completion of carbonation binder manufacturing, the timing of carbonation binder discharge of the carbonation reaction device (1) can be determined. After the discharge timing is determined, the aforementioned discharge valve (112a) is turned on so that the carbonation binder can be discharged.

[0422] Additionally, the carbonation reaction device (1) further includes a flow meter (18) capable of measuring the amount of carbon dioxide injected between the carbon dioxide injection part (15) and the main body (1212), and can control the number of times the liquid mixed binder repeatedly passes through the reaction part (121) through the amount of carbon dioxide injected measured through the flow meter (18).

[0423] For example, similar to the control method through the temperature measuring device (17) described above, the amount of carbon dioxide required to reach a preset reaction amount of the liquid mixed binder can be set through testing and calculation, etc., and when the amount of carbon dioxide measured through the flow meter (18) reaches the preset amount, the carbonation reaction device (1) can be controlled so that the liquid mixed binder stops passing through the reaction section (121) and is discharged through the second discharge section (112). For example, if it is expected that the progress of the carbonation reaction will be significantly slowed down when the preset amount is exceeded, discharge control to the second discharge section (112) can be performed when the preset amount is reached.

[0424] Additionally, a carbon dioxide pressurized supply device (not shown) and a CO2 flow meter (18) may be installed between the carbon dioxide injection unit (15) (line (injection pipe)) that supplies gaseous carbon dioxide from the gaseous carbon dioxide storage tank of the carbonation reaction device (1) to the reaction unit (121) (tubular mixing device) and the pump (122a). By directly measuring the amount of carbon dioxide supplied with the CO2 flow meter (18) and recognizing the completion of carbonation binder manufacturing through control, the timing of carbonation binder discharge from the carbonation reaction device (1) can be determined. Furthermore, when supplying carbon dioxide to the circulation transfer device (12), the carbon dioxide pressurized supply device, which controls the required pressure and amount for injection, can inject carbon dioxide at a certain pressure level so that it is faster than the rate at which the liquid mixed binder reacts with carbon dioxide. For example, the carbon dioxide pressurized supply device may be equipped with a solenoid valve.

[0425] In addition, the carbon dioxide pressurized supply device may be an air compressor, or the aforementioned pressure reducing device or the aforementioned gaseous carbon dioxide storage tank. It may be a method of supplying to the carbonation reaction device (1) using the self-pressure of the pressure reducing device or the gaseous carbon dioxide storage tank.

[0426] FIG. 30 is a drawing for explaining the case where a plurality of carbonation reaction devices (1) are provided in the second aspect of the present invention or in the seventh aspect to be described later.

[0427] Additionally, referring to FIG. 30, in step S12, the carbonation reaction device (1) may be provided in multiple units. Specifically, in step S12, the carbon dioxide buffer storage tank (14) is provided to be shared with the multiple carbonation reaction devices (1), and the second discharge unit (112) of each of the multiple carbonation reaction devices (1) is connected, and the multiple carbonation reaction devices (1) may be provided in an alternating circulation method that alternately discharges the carbonation binder in the order in which the carbonation binder is manufactured.

[0428] Specifically, referring to FIG. 30, a plurality of carbonation reaction devices (1) may be configured to share devices related to carbon dioxide injection. For example, as shown in FIG. 30, a carbon dioxide buffer storage tank (14), a vaporizer (13), a liquid carbon dioxide storage tank, etc., may be configured to be shared by a plurality of carbonation reaction devices (1).

[0429] Additionally, a plurality of carbonation reaction devices (1) can alternately and continuously transport carbonation binders in which the carbonation reaction is completed. For example, referring to FIG. 30, among the plurality of carbonation reaction devices (1), the carbonation reaction device (1) in which the carbonation binder is manufactured is discharged first, and then the carbonation binder in the remaining carbonation reaction devices (1) can be discharged when the manufacturing of the carbonation binder is completed.

[0430] For example, as described above, if the temperature inside the binder chamber (11) measured by the temperature measuring device (17) of one of the plurality of carbonation reaction devices (1) is above a preset temperature, or if the amount of carbon dioxide injected measured by the flow meter (18) reaches a preset amount of carbon dioxide injection, the manufacturing is considered complete, and the carbonation binder is discharged through the second discharge unit (112), and the carbonation binder can be manufactured in the remaining one of the plurality of carbonation reaction devices (1). At this time, the completion of manufacturing may mean that the reaction has been carried out for a longer time than the preset time as described above, or that the liquid mixed binder has circulated through the reaction unit (121) more than the preset number of times, or that the reaction has been carried out for a longer amount than the preset amount. In other words, if the progress of the carbonation reaction is expected to slow down significantly when exceeding a specific preset standard (temperature inside the chamber, amount of carbon dioxide injected, number of cycles, etc.), the time when the said preset standard is reached may be considered as the completion of manufacturing.

[0431] In addition, the single circulation method refers to a method in which the carbonation reaction is repeatedly caused by the circulation flow of the liquid mixed binder to complete the manufacture of the carbonation binder, and the carbonation binder is discharged all at once. It may be a unit carbonation reaction device (1) consisting of a single carbonation reaction device (1) as described above. This may be identical to the batch method in terms of producing and supplying the carbonation binder.

[0432] The alternating circulation method refers to a method in which two or more unit carbonation reaction devices (1) are provided and the carbonation binder is discharged alternately in the order in which it is manufactured. The number of unit carbonation reaction devices (1) can be set by considering the discharge amount and production time of the unit carbonation reaction devices (1) so that continuous production and supply of carbonation binder is possible.

[0433] For example, in a deep mixing process that requires a stable mass supply of materials, a carbonation reaction device (1) capable of continuous material supply that can continuously produce carbonation binder by a constant flow rate must be provided.

[0434] Furthermore, since the civil engineering sector requires a large workforce and large-scale specialized equipment, shortening the construction period and reducing waiting and maintenance times is a critical factor in terms of construction costs. To reduce the construction period, materials must be supplied in accordance with the efficiency of the construction equipment. Continuously supplying materials is the best way to increase construction equipment efficiency by utilizing the equipment continuously. Since a single-circulation system may result in downtime, an alternating circulation system must be applied to enable the continuous supply of carbonation binders. As deep mixing equipment such as DCM is expensive and large-scale machinery, the production and supply of carbonation binders must proceed continuously and stably to maximize equipment efficiency, thereby minimizing both construction costs and time.

[0435] When manufacturing a carbonation binder using the above-described manufacturing method (S1), carbonation can be contributed to carbon neutrality by utilizing captured carbon dioxide.

[0436] In addition, the manufacturing method (S1) can contribute to carbon neutrality by storing the captured carbon dioxide.

[0437] In addition, the manufacturing method (S1) can contribute to carbon neutrality by reducing the use of cement and suppressing the generation of carbon dioxide.

[0438] In addition, the manufacturing method (S1) can increase economic and environmental benefits in various aspects by utilizing carbon dioxide to increase the strength of the soft ground improvement, thereby reducing the amount of binder used, reducing transportation and storage costs due to the reduced amount of binder used, reducing carbon dioxide emissions during transportation due to the reduced amount of binder transported, reducing carbon dioxide emissions during cement production due to the reduced amount of binder used, and acquiring carbon emission rights.

[0439] <Deep mixing treatment method for soft ground improvement according to the third aspect of the present invention>

[0440] Hereinafter, a deep mixing treatment method for soft ground improvement according to the third aspect of the present invention (hereinafter referred to as the 'deep mixing treatment method (S2)') will be described. However, the deep mixing treatment method (S2) relates to a deep mixing treatment method for soft ground improvement that includes a carbonation binder manufacturing method according to the first aspect of the present invention or a carbonation binder manufacturing method according to the second aspect of the present invention. Since it shares the same or corresponding technical features as the carbonation binder manufacturing method according to the first aspect of the present invention and the carbonation binder manufacturing method according to the second aspect of the present invention, the same reference numerals will be used for components that are identical or similar to the carbonation binder manufacturing method according to the first aspect of the present invention or the carbonation binder manufacturing method according to the second aspect of the present invention, and redundant descriptions will be simplified or omitted.

[0441] However, below, the deep mixing treatment method for soft ground improvement according to the third aspect of the present invention will be explained based on FIGS. 31 and FIGS. 32 (drawings corresponding to the deep mixing treatment method for soft ground improvement according to the third aspect of the present invention).

[0442] Here, deep mixing treatment refers to a ground improvement method that stabilizes and strengthens soft original ground composed of clayey soil, sandy soil, organic soil, etc., by transporting a liquid binder, which is a mixture of powdered binder (cement, blast furnace slag, etc.) and water, and injecting it into the ground in that state while rotating and mixing it with a stirrer. Wet ground improvement methods carried out at a depth of 4m or more from the surface on land or at sea, such as the DCM (Deep Cement Mixing Method) method, which is primarily intended for reinforcing bearing capacity, and the SCW (Soil Cement Wall) method, which is primarily intended for waterproofing, can all be classified as deep mixing treatment methods. Here, "wet" means using a liquid binder in the state of a powdered binder mixed with water, and it can be distinguished from dry ground improvement methods, which involve injecting and mixing the powdered binder as is.

[0443] FIG. 31 is a flowchart of a deep mixing treatment method for soft ground improvement according to the third aspect of the present invention.

[0444] Referring to FIG. 31, the deep mixing treatment method (S2) may include a step (S21) of manufacturing a carbonated binder by the manufacturing method (S1) according to the first or second aspect of the present invention.

[0445] At this time, step S21 may include the step of mixing the aforementioned powdered binder and mixing water to produce a liquid mixed binder, and the step of producing a carbonated binder by reacting the liquid mixed binder produced by a carbonation reaction device (the carbonation reaction device (100) described in the description of the first aspect of the present invention or the carbonation reaction device (1) described in the description of the second aspect of the present invention) with carbon dioxide.

[0446] In other words, step S21 may be a step of making a liquid mixed binder by mixing a powdered binder and a mixture of water in a certain ratio, and making a carbonated binder by reacting the liquid mixed binder with CO2 using a carbonation reaction device (the carbonation reaction device (100) described in the description of the first aspect of the present invention or the carbonation reaction device (1) described in the description of the second aspect of the present invention).

[0447] At this time, the carbonation reaction device (100) described in the description of the first aspect of the present invention is a continuous flow type and is provided to be sealed from the atmosphere, and the liquid mixed binder may be provided with a powdered binder having a fineness of 2,000 cm2 / g (Blaine) or more and a mixed water with a weight ratio of water to the powdered binder of 70% or more and 120% or less so that a certain level of flow rate can be achieved.

[0448] In addition, the carbonation reaction device (1) described in the description of the second aspect of the present invention is a circulating manufacturing method, and the liquid mixed binder may be provided with a powdered binder having a fineness of 2,000 cm2 / g (Blaine) or more (preferably 2,500 cm2 / g (Blaine) or more, more preferably 3,000 cm2 / g (Blaine) or more) and a pH of 12, and a mixed water having a weight ratio of water to the powdered binder of 70% or more and 120% or less.

[0449] In addition, for deep mixing treatment for soft ground improvement, the ratio of mixing water (W / B) specified in the specifications is 70% to 120%. The DCM can be 70% to 120%, preferably 60% to 100%.

[0450] Figure 32 is a drawing to explain the results of comparing the strength of a carbonated DCM mold to which the present invention is applied and a general DCM mold.

[0451] Referring to Fig. 32, the present invention compared the strength of a conventional DCM mold and a carbonated DCM mold to which the present technology was applied, using the same soil sample, binder, and mixing water for soft ground deep mixing treatment (DCM). As shown in Fig. 32, it can be confirmed that the carbonated DCM mold has a compressive strength approximately 1.5 times higher than that of a conventional DCM mold. From the above experimental results, it can be seen that compressive strength is increased by carbonation, and it can be inferred that the present invention makes it possible to reduce the amount of cement used at an equivalent level of strength.

[0452] Step S21 has been described in detail through the explanation of the manufacturing method (S1) in the first and second aspects of the present invention, so a more specific explanation will be omitted.

[0453] Additionally, referring to FIG. 31, the deep mixing treatment method (S2) may include a step (S22) of preparing a carbonation mixture by stirring a carbonation binder with the original ground soil.

[0454] In other words, in step S22, a carbonation binder can be mixed with the original ground soil to create a carbonation mixture.

[0455] At this time, the deep mixing treatment method (S2) may include a step of transporting the manufactured carbonation binder to the original ground improvement work location by means of a carbonation binder transport device between step S21 and step S22.

[0456] Typically, in the DCM method, the mix consists of a soil moisture content of 90% to 110%, a soil unit weight of 1400 to 1600 kg / m³ (1550 kg), a binder mix amount of 245 kg / m³ (slag cement) (245 kg), and a water-to-binder ratio of 70% to 100% (196 kg). The weight ratio of the soil, binder, and water is approximately 78:12:10, and the volume ratio is 78:7:15.

[0457] In addition, the deep mixing treatment method (S2) may include a step (S23) of curing the carbonation mixture to produce a soft ground improvement body.

[0458] The process of curing the carbonation mixture in step S23 is obvious to a person skilled in the art, so a more detailed explanation will be omitted.

[0459] <Deep mixing treatment soft ground improvement using carbon dioxide according to the 4th aspect of the present invention>

[0460] Meanwhile, the soft ground improvement material using deep mixing treatment with carbon dioxide according to the fourth aspect of the present invention can be produced by the deep mixing treatment method for soft ground improvement according to the third aspect of the present invention.

[0461] In other words, the deep mixing treatment soft ground improvement body can be produced through the steps of: mixing a powdered binder and a mixing water in a certain ratio using the deep mixing treatment method (S2) to create a liquid mixed binder; reacting the liquid mixed binder with CO2 using a carbonation reaction device (1 or 100) to create a carbonated binder; transporting the carbonated binder to the original ground improvement work location; mixing the carbonated binder with the original ground soil to create a carbonated mixture; and curing the carbonated mixture to create a soft ground improvement body.

[0462] <Method for manufacturing concrete comprising a carbonation binder according to the fifth aspect of the present invention>

[0463] Hereinafter, a method for manufacturing concrete including a carbonation binder according to the fifth aspect of the present invention (hereinafter referred to as the 'method for manufacturing concrete (S3)') will be described. However, the method for manufacturing concrete (S3) relates to a method for manufacturing concrete including a carbonation binder according to the first aspect of the present invention or a carbonation binder according to the second aspect of the present invention, and since it shares the same or corresponding technical features as the method for manufacturing a carbonation binder according to the first aspect of the present invention or the method for manufacturing a carbonation binder according to the second aspect of the present invention, the same reference numerals will be used for components that are identical or similar to the components of the method for manufacturing a carbonation binder according to the first aspect of the present invention or the method for manufacturing a carbonation binder according to the second aspect of the present invention, and redundant descriptions will be simplified or omitted.

[0464] However, below, a method for manufacturing concrete containing a carbonation binder according to the fifth aspect of the present invention will be described based on FIG. 33 (a flowchart for a method for manufacturing concrete containing a carbonation binder according to the fifth aspect of the present invention).

[0465] FIG. 33 is a flowchart of a method for manufacturing concrete containing a carbonation binder according to the fifth aspect of the present invention.

[0466] Referring to FIG. 33, the concrete manufacturing method (S3) may include a step (S31) of manufacturing a carbonated binder by the manufacturing method (S1) according to the first aspect of the present invention or the second aspect of the present invention.

[0467] In step S31, the weight ratio (W / B) of the mixing water to the powdered binder specified in the specifications is 20~25% for high-strength concrete and 40~65% for ordinary concrete. In the case of high-strength concrete, instead of reducing the mixing water ratio, admixtures for fluidity (AE agents, water reducers, high-performance AE water reducers, etc.) may be added.

[0468] When manufacturing concrete, the ratio of the water of the liquid mixed binder to the powdered binder may be smaller than in the case of DCM. This is because the required strength is much higher than in the case of DCM, and there may be cases where the W / B ratio is less than 50%. In this case, in order to secure the circulation flow rate of the carbonation reaction device (1), the carbonation binder can be partially manufactured using the liquid mixed binder produced with 50% or more of water, and then the powdered binder is added to the manufactured carbonation binder and mixed to meet the required W / B ratio and produce the carbonation mixture.

[0469] In addition, the step (S31) of manufacturing the carbonation binder has been described in detail through the manufacturing method (S1) according to the first aspect of the present invention and the manufacturing method (S1) according to the second aspect of the present invention, so a more detailed explanation will be omitted.

[0470] Referring to FIG. 33, the concrete manufacturing method (S3) may include a step (S32) of manufacturing concrete by mixing the manufactured carbonation binder with aggregate.

[0471] In other words, in step S32, the carbonation binder prepared in step S31 can be stirred with aggregate to create a carbonation mixture.

[0472] At this time, the concrete manufacturing method (S3) may include a step of transporting the manufactured carbonated binder to the aggregate mixing location by means of a carbonated binder transport device between steps S31 and S32.

[0473] The above carbonation binder transfer device may be equipped with a flow control device capable of buffering and adjusting the carbonation binder manufacturing speed in step S31 and the carbonation mixture manufacturing speed in step S32. The flow control device may include a carbonation binder temporary storage tank, a transfer pump (122a), and a valve, etc.

[0474] In addition, the concrete produced in step S32 can be poured into the required space and cured thereafter.

[0475] In addition, the present invention can also provide concrete (including both unhardened and hardened (cured) states) manufactured by the concrete manufacturing method (S3).

[0476] <Concrete member using carbon dioxide according to the 6th aspect of the present invention>

[0477] Meanwhile, a concrete member using carbon dioxide according to the 6th aspect of the present invention can be produced by the concrete manufacturing method (S3) including a carbonation binder according to the 5th aspect of the present invention.

[0478] In other words, the present invention can provide a concrete member (a concrete member using carbon dioxide) comprising concrete manufactured by the concrete manufacturing method (S3). Here, the term "concrete member" can be broadly understood to encompass not only various member forms obvious to a person skilled in the art, but also structural forms including the member.

[0479] <Carbonation reaction apparatus according to the 7th aspect of the present invention>

[0480] Hereinafter, a carbonation reaction apparatus (1) according to the seventh aspect of the present invention will be described. However, since the carbonation reaction apparatus (1) relates to an apparatus used in the method for manufacturing a carbonation binder according to the second aspect of the present invention and shares the same or corresponding technical features as the method for manufacturing a carbonation binder according to the second aspect of the present invention, the same reference numerals will be used for configurations that are identical or similar to the configuration of the method for manufacturing a carbonation binder according to the second aspect of the present invention, and redundant descriptions will be simplified or omitted.

[0481] For reference, the method for manufacturing a carbonation binder according to the second aspect of the present invention described above was explained based on FIGS. 1 to 4 (for reference, FIGS. 1 to 4 are drawings that are commonly applied to the first and second aspects of the present invention) and FIGS. 16 to 30 (drawings corresponding to the method for manufacturing a carbonation binder according to the second aspect of the present invention).

[0482] Referring to FIGS. 16, 19, 22, 26 and 29, the carbonation reaction device (1) may include a binder chamber (11) comprising a second input section (111) into which a liquid mixed binder is introduced and a second discharge section (112) for discharging at least a portion of the reacted liquid mixed binder.

[0483] Specifically, the binder chamber (11) may include a chamber body (113) connected to a second input section (111) into which a liquid mixed binder is introduced, a second discharge section (112) into which a carbonated binder is discharged, and a circulation transfer device (12).

[0484] Additionally, the second input section (111) may be equipped with an input valve (111a) capable of controlling the amount of liquid mixed binder to be input. For example, the input valve (111a) may be provided as a proportional control valve or a controllable on / off (open / close valve).

[0485] Additionally, the second discharge section (112) may be equipped with a discharge valve (112a) capable of controlling the discharge amount of the carbonated binder produced by completing the carbonation reaction of the liquid mixed binder. For example, the discharge valve (112a) may be provided as a proportional control valve or a controllable on / off (open / close valve).

[0486] Additionally, the binder chamber (11) (specifically the chamber body (113)) may be a box-shaped chamber with a square cross section, the binder chamber (11) may be a circular pipe with the same diameter as the transfer pipe (123) of the circulating transfer device (12) described later, and the binder chamber (11) may be a T-shaped composite chamber equipped with a transfer pipe (123) connected vertically downward to an upper horizontal cylindrical chamber.

[0487] Referring to FIGS. 17 and 18, the binder chamber (11) may be configured so that the liquid mixed binder within the binder chamber (11) flows spirally toward the second discharge section (112) of the binder chamber (11). Specifically, the binder chamber (11) may be configured in a cone shape with a diameter that decreases along the direction toward the second discharge section (112) of the binder chamber (11), and the reaction section (121) may be connected circumferentially so that the liquid mixed binder reacted with carbon dioxide flows spirally inside the binder chamber (11).

[0488] Additionally, with reference to FIGS. 16, 17, 19, 22, 26, and 29, the carbonation reaction device (1) may include a circulation transfer device (12) connected to a binder chamber (11) and including a reaction section (121) in which the introduced liquid mixed binder reacts with carbon dioxide.

[0489] At this time, with reference to FIGS. 16, 17, 19, 22, 26 and 29, in step S12, a carbonated binder can be produced by reacting a liquid mixed binder with carbon dioxide through a pump (122a) (specifically, a venturi pump (122a) to be described later) and a reaction unit (121) while passing through a circulation transfer device (12).

[0490] Additionally, referring to FIGS. 16 and 17, the circulating transfer device (12) may include a reaction section (121), an inlet section (122) connected to the binder chamber (11) through which a liquid mixed binder is introduced from the binder chamber (11), and a transfer pipe (123) provided to allow the liquid mixed binder introduced into the inlet section (122) to move toward the reaction section (121). Here, the reaction section (121) may include a third input section (1211) connected to the transfer pipe (123) and into which the liquid mixed binder that has moved along the transfer pipe (123) is introduced, a main body (1212) into which the introduced liquid mixed binder reacts with carbon dioxide, and a third discharge section (1213) into which at least a portion of the reacted liquid mixed binder is discharged to the binder chamber (11).

[0491] Additionally, carbon dioxide may be supplied to the reaction unit (121) by a carbon dioxide injection unit (15) connected to the circulation transport device (12). Specifically, referring to FIG. 16, a carbon dioxide injection unit (15) that injects carbon dioxide directly or indirectly into the reaction unit (121) may be connected to the circulation transport device (12).

[0492] Additionally, referring to FIG. 16, the circulation transfer device (12) is connected to a liquid carbon dioxide storage tank, a vaporizer (13), and a pressure reducing device so that gaseous carbon dioxide can be injected.

[0493] At this time, the pressure reduction device includes a carbon dioxide buffer storage tank (14) that buffers and stores the reduced pressure gaseous carbon dioxide, and the carbon dioxide buffer storage tank (14) may be configured to maintain a pressure within a preset pressure range.

[0494] Additionally, referring to FIGS. 16 and 17, a carbon dioxide recovery pipe (16) may be connected to the binder chamber (11) so that carbon dioxide that has not reacted with the liquid mixed binder among the carbon dioxide injected from the carbon dioxide injection unit (15) is recovered into the carbon dioxide buffer storage tank (14).

[0495] Additionally, the inlet section (122) may include an inlet connected to the binder chamber (11) and a pump (122a) provided to apply pressure to introduce the liquid mixed binder into the reaction section (121).

[0496] Additionally, referring to FIGS. 19 to 21, the main body (1212) may include a static mixer section (12121) that includes a static mixer (12121a) provided inside the passage to induce turbulent mixing for a liquid mixed binder that is discharged to a third discharge section (1213) connected to the other side, passing through a passage that is directly or indirectly connected to a third input section (1211) and a carbon dioxide injection section (15) on one side.

[0497] Additionally, referring to FIGS. 22 to 24 as another example, the main body (1212) includes a venturi tube section (12122) provided in the form of a venturi tube, a third input section (1211) (liquid mixing binder inlet section (122)) is connected to one side of the venturi tube, a third discharge section (1213) (outlet section) is connected to the other side of the venturi tube, and a carbon dioxide injection section (15) may be provided so as to be located closer to the minimum cross-section position among the position where the passage cross-section of the tube is the maximum cross-section and the position where the minimum cross-section is the minimum cross-section in the venturi tube.

[0498] In addition, the single venturi tubes shown in FIGS. 23 and 24 can all be replaced with multi-venturi tubes as shown in FIG. 25.

[0499] As another example, referring to FIGS. 26 and 27, the reaction section (121) of the circulation transfer device (12) may include a venturi tube section (12122) which is configured in the form of a venturi tube with one side connected to a third input section (1211) and a carbon dioxide injection section (15) connected in the middle, and a static mixer section (12121) which is configured in the form of a static mixer (12121a) with one side connected to the other side of the venturi tube section (12122) and connected to a third discharge section (1213) (outflow section) on the other side. For example, referring to FIG. 27, the static mixer section (12121) configured in the form of a static mixer (12121a) may be formed between the venturi tube section (12122) and the third discharge section (1213).

[0500] Additionally, referring to FIGS. 28 and 29, the aforementioned pump (122a) may be a venturi pump (122a) provided to inject carbon dioxide at a pressure higher than a preset pressure and to apply pressure such that a liquid mixed binder is injected into the main body (1212) by the vacuum generated through the injection of carbon dioxide at a pressure higher than the preset pressure.

[0501] Additionally, with reference to FIGS. 16, 17, 19, 22, 26, and 29, the carbonation reaction device (1) includes a temperature measuring device (17) for measuring the temperature inside the binder chamber (11), and the number of times the liquid mixed binder repeatedly passes through the reaction section (121) can be controlled through the temperature measured by the temperature measuring device (17).

[0502] Additionally, the carbonation reaction device (1) further includes a flow meter (18) capable of measuring the amount of carbon dioxide injected between the carbon dioxide injection part (15) and the main body (1212), and can control the number of times the liquid mixed binder repeatedly passes through the reaction part (121) through the amount of carbon dioxide injected measured through the flow meter (18).

[0503] Additionally, the carbonation reaction device (1) may be provided to follow a circulating flow method in which the liquid mixed binder contained in the binder chamber (11) repeatedly passes through the reaction section (121).

[0504] Referring to FIG. 16, the circulation flow may refer to a flow in which the liquid mixed binder repeatedly reacts with carbon dioxide in the reaction section (121).

[0505] Additionally, referring to FIG. 30, the carbonation reaction device (1) may be provided in multiple units. Specifically, the carbon dioxide buffer storage tank (14) is provided to be shared with the multiple carbonation reaction devices (1), and the second discharge unit (112) of each of the multiple carbonation reaction devices (1) is connected, and the multiple carbonation reaction devices (1) may be provided in an alternating circulation method that alternately discharges the carbonation binder in the order in which the carbonation binder is manufactured.

[0506] <Carbon dioxide capture device according to the 8th aspect of the present invention>

[0507] Hereinafter, a carbon dioxide capture device (2) according to the eighth aspect of the present invention will be described. However, since the carbon dioxide capture device (2) utilizes a carbonation reaction device (1) and shares the same or corresponding technical features as the carbonation reaction device (1), the same reference numerals will be used for configurations that are identical or similar to the configuration of the carbonation reaction device (1), and redundant descriptions will be simplified or omitted.

[0508] Specifically, the carbon dioxide capture device (2) is a device implemented through a circulating flow method, similar to the carbonation reaction device (1) described above, and the two devices can be said to share the same or corresponding technical features. However, while the carbonation reaction device (1) described above corresponds to a device that processes carbon dioxide collected by manufacturing a carbonation binder using carbon dioxide, the carbon dioxide capture device (2) can be understood as a device that captures at least a portion of the carbon dioxide contained in the carbon dioxide-containing gas, such as air or exhaust gas, by reacting (contacting) it with a liquid carbon dioxide absorbent.

[0509] Accordingly, the configurations applied to the carbonation reaction device (1) described above may be applied to the carbon dioxide capture device (2) in the same or similar manner, and can be understood by referring to the description of the carbon dioxide capture device (2).

[0510] However, below, the carbon dioxide capture device according to the eighth aspect of the present invention will be described based on FIGS. 18 to 20, FIGS. 22, FIGS. 23, FIGS. 26 to 29 (for reference, FIGS. 18 to 20, FIGS. 22, FIGS. 23, FIGS. 26 to 29 are drawings showing a configuration identical or similar to the configuration of the carbon dioxide capture device according to the eighth aspect of the present invention among the configurations of the carbonation reaction device (1) according to the second aspect of the present invention) and FIG. 34 (a drawing corresponding to the carbon dioxide capture device according to the eighth aspect of the present invention).

[0511] Additionally, components assigned with a reference numeral attached to the reference numeral can be understood by referring to the components assigned with a reference numeral not attached to the carbonation reaction device (1) described above. For example, the absorber chamber (11') is a component corresponding to the binder chamber (11) described above, and can be applied in the same or similar manner as the components applied to the binder chamber (11). Likewise, the carbon dioxide-containing gas injection unit (15') is a component corresponding to the carbon dioxide injection unit (15), and can be applied in the same or similar manner as the components applied to the carbon dioxide injection unit. Accordingly, a more detailed description of the components included in the carbon dioxide capture device (2) will be omitted.

[0512] FIG. 34 is a drawing for explaining a carbon dioxide capture device (2) using a carbonation reaction device (1) according to the eighth aspect of the present invention.

[0513] Referring to FIG. 34, the carbon dioxide capture device (2) may include an absorbent chamber (11') comprising a second input section (111) into which a liquid carbon dioxide absorbent is introduced and a second discharge section (112) for discharging at least a partially reacted liquid carbon dioxide absorbent.

[0514] At this time, the liquid carbon dioxide absorbent may contain one or more of NaOH, KOH, MEA (monoethanolamine), and zeolite.

[0515] Additionally, the absorbent chamber (11') (specifically, the absorbent chamber body (113')) may be a box-shaped chamber with a square cross section, and the absorbent chamber (11') may be a circular pipe with the same diameter as the transfer pipe (123) of the circulation transfer device (12) described later, and the absorbent chamber (11') may be a T-shaped composite chamber equipped with a transfer pipe (123) connected vertically downward to an upper horizontal cylindrical chamber.

[0516] Additionally, the second input section (111) may be equipped with an input valve (111a) capable of controlling the amount of liquid carbon dioxide absorbent input. For example, the input valve (111a) may be provided as a proportional control valve or a controllable on / off (open / close valve).

[0517] Additionally, the second discharge section (112) may be equipped with a discharge valve (112a) capable of controlling the discharge amount of the liquid carbon dioxide absorbent that has reacted with a gas (air, exhaust gas) containing carbon dioxide. For example, the discharge valve (112a) may be provided as a proportional control valve or a controllable on / off valve.

[0518] Additionally, referring to FIG. 34, the carbon dioxide capture device (2) may include a circulation transfer device (12) connected to an absorber chamber (11') and including a reaction section (121) in which the introduced liquid carbon dioxide absorber reacts with carbon dioxide of a carbon dioxide-containing gas.

[0519] Here, the carbon dioxide-containing gas may be air or exhaust gas. However, it is not limited to this, and it goes without saying that various gases containing carbon dioxide, in which at least some carbon dioxide can be captured by the carbon dioxide capture device (2), may be included.

[0520] Additionally, carbon dioxide-containing gas may be injected into the reaction section (121) by a carbon dioxide-containing gas injection section (15') connected to the circulation transport device (12). In other words, a carbon dioxide-containing gas injection section (15') that injects carbon dioxide-containing gas (air, exhaust gas) directly or indirectly into the reaction section (121) may be connected to the circulation transport device (12).

[0521] At this time, unreacted gas can be released into the air.

[0522] Additionally, referring to FIG. 34, the circulating transfer device (12) may include a reaction section (121), an inlet section (122) connected to an absorbent chamber (11') into which a liquid carbon dioxide absorbent is introduced, and a transfer pipe (123) provided to allow the liquid carbon dioxide absorbent introduced into the inlet section (122) to move toward the reaction section (121). Here, the reaction section (121) may include a third input section (1211) connected to the transfer pipe (123) and into which the liquid carbon dioxide absorbent that has moved along the transfer pipe (123) is introduced, a main body (1212) into which the introduced liquid carbon dioxide absorbent reacts with a gas (air, exhaust gas) containing carbon dioxide, and a third discharge section (1213) into which at least a portion of the reacted liquid carbon dioxide absorbent is discharged to the absorbent chamber (11').

[0523] Referring to FIG. 18 and FIG. 34 together, the third discharge section (1213) is connected to form a spiral flow of liquid carbon dioxide absorbent discharged therefrom proceeding spirally along the direction of gravity within the absorber chamber (11'), and the inlet section (122) can be connected to the absorber chamber (11') below the third discharge section (1213) to implement a circulating flow method.

[0524] Specifically, referring to FIG. 18 and FIG. 34, the absorber chamber (11') (specifically, the absorber chamber body (113')) is provided in a cone shape with a diameter that decreases as it goes downward, and the third discharge part (1213) can be connected to the inside of the absorber chamber (11') so that a liquid carbon dioxide absorbent that has reacted with carbon dioxide at least partially is discharged in the circumferential direction or tangential direction of the absorber chamber (11').

[0525] Additionally, referring to FIG. 34, the inlet (122) may include an inlet connected to the absorbent chamber (11') and a pump (122a) provided to apply pressure to introduce the liquid carbon dioxide absorbent into the reaction section (121).

[0526] Additionally, the carbon dioxide capture device (2) may be provided to follow a circulating flow method in which a liquid carbon dioxide absorbent contained within an absorbent chamber (11') repeatedly passes through a reaction section (121).

[0527] The circulation flow may refer to a flow in which a liquid carbon dioxide absorbent repeatedly passes through the reaction section (121) to react with a gas containing carbon dioxide (air, exhaust gas).

[0528] Referring together to FIGS. 19, 20 and 34, the main body (1212) may include a static mixer section (12121) that includes a static mixer (12121a) provided inside the passage to induce turbulent mixing for a liquid carbon dioxide absorbent discharged to a third discharge section (1213) connected to the other side, passing through a passage that is directly or indirectly connected to a third input section (1211) and a gas injection section (15) on one side.

[0529] Additionally, referring to FIGS. 22, 23, and 34 together as another example, the main body (1212) includes a venturi tube section (12122) provided in the form of a venturi tube, a third inlet (1211) (liquid carbon dioxide absorbent inlet (122)) is connected to one side of the venturi tube, a third outlet (1213) (outlet) is connected to the other side of the venturi tube, and a carbon dioxide-containing gas injection part (15') may be provided so as to be located closer to the minimum cross-section position among the position where the passage cross-section of the tube is the maximum cross-section and the position where the minimum cross-section is the minimum cross-section in the venturi tube.

[0530] As another example, referring to FIGS. 26, 27, and 34 together, the reaction section (121) of the circulation transfer device (12) may include a venturi tube section (12122) which is configured in the form of a venturi tube with one side connected to a third input section (1211) and a carbon dioxide-containing gas injection section (15') connected in the middle, and a static mixer section (12121) which is configured in the form of a static mixer (12121a) with one side connected to the other side of the venturi tube section (12122) and connected to a third discharge section (1213) (outflow section) on the other side. The static mixer section (12121) configured in the form of a static mixer (12121a) may be formed between the venturi tube section (12122) and the third discharge section (1213).

[0531] Additionally, referring to FIGS. 28, 29 and 34 together, the pump (122a) may be a venturi pump (122a) provided to inject a gas containing carbon dioxide at a pressure above a preset pressure and to apply pressure such that a liquid carbon dioxide absorbent is introduced into the main body (1212) through the vacuum generated by injecting the gas containing carbon dioxide at a pressure above the preset pressure.

[0532] The foregoing description of the present invention is for illustrative purposes only, and those skilled in the art will understand that other specific forms can be easily modified without altering the technical concept or essential features of the present invention. Therefore, the embodiments described above should be understood as illustrative in all respects and not restrictive. For example, each component described as a single unit may be implemented in a distributed manner, and components described as distributed may likewise be implemented in a combined form.

[0533] The scope of the present invention is defined by the claims set forth below rather than by the detailed description above, and all modifications or variations derived from the meaning and scope of the claims and the concept of equivalents thereof should be interpreted as being included within the scope of the present invention.

Claims

1. A method for manufacturing a carbonate binder, (a) a step of mixing a powdered binder with water to produce a liquid mixed binder; and (b) a step of producing a carbonation binder by reacting the liquid mixed binder produced by a carbonation reaction device with carbon dioxide, wherein the method comprises: A method for manufacturing a carbonation binder, wherein the carbonation reaction apparatus is provided to follow a continuous flow method in which the liquid mixed binder is introduced, reacts with carbon dioxide, and discharged sequentially.

2. In Paragraph 1, A method for manufacturing a carbonated binder, wherein, in step (a) above, the liquid mixed binder is produced by including a powdered binder with a fineness of 2,000 cm2 / g (Blaine) or more and a mixed water with a weight ratio of water to the powdered binder of 70% or more and 120% or less, taking into account the flow in the continuous flow method of step (b) above.

3. In Paragraph 1, A method for manufacturing a carbonation binder, wherein in step (b) above, the carbonation reaction device is connected to a liquid carbon dioxide storage tank, a vaporizer, and a pressure reducing device so that gaseous carbon dioxide is injected.

4. In Paragraph 3, The above-mentioned pressure reduction device includes a carbon dioxide buffer storage tank that buffers and stores the reduced-pressure gaseous carbon dioxide, and A method for manufacturing a carbonation binder, wherein the carbon dioxide buffer storage tank is configured to maintain pressure within a preset pressure range.

5. In Paragraph 1, The above carbonation reaction device is, An input section into which a liquid mixed binder is introduced; A main body in which an injected liquid mixed binder reacts with CO2; A discharge portion having a discharge port through which at least a portion of the reacted liquid mixed binder is discharged; and A method for manufacturing a carbonation binder comprising a carbon dioxide injection unit for injecting carbon dioxide into the above-mentioned main body.

6. In Paragraph 5, The above-mentioned input section includes an input port connected to the main body, a transfer pipe connected to the input port, and a pump provided to apply pressure to inject a liquid mixed binder into the main body. A method for manufacturing a carbonation binder, wherein the inlet port is closed by the liquid mixed binder being introduced and the outlet port is closed by the liquid mixed binder being discharged, and the interior of the main body is controlled to follow the continuous flow method while maintaining a closed state that is closed above a preset level of closure.

7. In Paragraph 5, A method for manufacturing a carbonation binder, wherein, in step (b) above, a negative pressure corresponding to at least a portion of the pressure required to inject carbon dioxide into the main body is formed in the carbon dioxide injection part due to a vacuum phenomenon caused by a carbonation reaction between the liquid mixed binder and carbon dioxide inside the main body.

8. In Paragraph 5, The above main body is, A method for manufacturing a carbonation binder, comprising a static mixer section including a static mixer provided inside a passage to induce turbulent mixing for a liquid mixed binder discharged to a discharge section connected to the other side, passing through a passage directly or indirectly connected to one side of the input section and the carbon dioxide injection section.

9. In Paragraph 5, The above main body includes a venturi tube section provided in the form of a venturi tube, and The above input part is connected to one side of the above Venturi tube, and The above discharge part is connected to the other side of the above Venturi tube, and A method for manufacturing a carbonation binder, wherein the carbon dioxide injection part is provided such that the cross-section of the passage of the tube in the venturi tube is positioned closer to the position of the minimum cross-section between the position of the maximum cross-section and the position of the minimum cross-section.

10. In Paragraph 5, The above main body is, A venturi tube section portion configured in the form of a venturi tube, with one side connected to the input portion and the carbon dioxide injection portion connected in the middle; and A method for manufacturing a carbonation binder, wherein one side is connected to the other side of the venturi tube section, the other side is connected to the discharge section, and includes a static mixer section provided in the form of a static mixer in the middle.

11. In Paragraph 5, The discharge portion of the above carbonation reaction device is connected to a carbon dioxide recovery device, and The above carbon dioxide recovery device is, A carbon dioxide separation chamber connected to the above discharge section and extending downward; and A method for manufacturing a carbonation binder, comprising a carbon dioxide recovery unit connected to the upper side of the carbon dioxide separation chamber.

12. In Paragraph 1, The above carbonation reaction device is, Multiple unit carbonation reactors are provided to be arranged in series, or Multiple unit carbonation reactors are provided to be arranged in parallel, or A method for manufacturing a carbonation binder, wherein a plurality of unit carbonation reaction devices are provided to be arranged in a matrix form that combines series and parallel.

13. In Paragraph 1, A method for manufacturing a carbonation binder, wherein the total length of the carbonation reaction apparatus is set to have a flow rate difference that maintains a continuous fluid flow with friction in a state where the carbon dioxide reaction proceeds beyond a preset reaction amount, taking into account the vacuum phenomenon that occurs during the reaction with carbon dioxide.

14. In Paragraph 13, The above carbonation reaction device includes a plurality of unit reaction devices connected in series, and The above unit reaction device includes a carbon dioxide injection unit and a static mixer, and A method for manufacturing a carbonation binder, wherein the length of each of the above-mentioned unit reaction devices is set to have a flow rate difference such that a continuous fluid flow is maintained with frictional considerations at a flow rate in a state where the carbon dioxide reaction proceeds beyond a preset reaction amount.

15. A method for manufacturing a carbonate binder, (a) a step of mixing a powdered binder with water to produce a liquid mixed binder; and (b) a step of producing a carbonation binder by reacting the liquid mixed binder produced by a carbonation reaction device with carbon dioxide, wherein the method comprises: The above carbonation reaction device is, A binder chamber comprising a first input section into which the generated liquid mixed binder is introduced and a first discharge section for discharging at least a portion of the reacted liquid mixed binder; and A circulating transfer device comprising a reaction section connected to the binder chamber and in which the introduced liquid mixed binder reacts with carbon dioxide, wherein The carbonation reaction apparatus is provided to follow a circulating flow method in which a liquid mixed binder contained within the binder chamber repeatedly passes through the reaction section, and A method for manufacturing a carbonation binder, wherein carbon dioxide is supplied to the reaction section by a carbon dioxide injection section connected to the circulation transfer device.

16. In Paragraph 15, A method for manufacturing a carbonation binder, wherein, in step (a) above, the liquid mixed binder is produced by including a powdered binder having a fineness of 2,000 cm2 / g (Blaine) or more and a pH of 10 or more, and a mixed water having a weight ratio of 50% or more to the powdered binder, taking into account the flow rate in the circulating flow method of step (b).

17. In Paragraph 15, A method for manufacturing a carbonation binder, wherein in step (b) above, the circulating transfer device is connected to a liquid carbon dioxide storage tank, a vaporizer, and a pressure reducing device so that gaseous carbon dioxide is injected.

18. In Paragraph 17, The above-mentioned pressure reduction device includes a carbon dioxide buffer storage tank that buffers and stores the reduced-pressure gaseous carbon dioxide, and A method for manufacturing a carbonation binder, wherein the carbon dioxide buffer storage tank is configured to maintain pressure within a preset pressure range.

19. In Paragraph 15, The above-mentioned circulation transfer device is, The above reaction unit; An inlet connected to the binder chamber and into which a liquid mixed binder is introduced from the binder chamber; and It includes a transfer pipe provided to move the liquid mixed binder introduced into the inlet to the reaction section, The above reaction unit is, A second input section connected to the above transfer pipe and into which the above liquid mixed binder, which has moved along the above transfer pipe, is introduced; A main body in which an introduced liquid mixed binder reacts with carbon dioxide; and A method for manufacturing a carbonation binder comprising a second discharge section in which at least some of the reacted liquid mixed binder is discharged into the binder chamber.

20. In Paragraph 19, The above circulation transfer device The carbon dioxide injection unit for directly or indirectly injecting carbon dioxide into the above reaction unit is connected, and In the binder chamber above, A method for manufacturing a carbonation binder, wherein a carbon dioxide recovery pipe is connected to recover carbon dioxide that has not reacted with the liquid mixed binder among the carbon dioxide injected from the carbon dioxide injection part to the carbon dioxide buffer storage tank.

21. In Paragraph 19, The above inlet part A method for manufacturing a carbonation binder, comprising an inlet connected to the binder chamber and a pump provided to apply pressure to introduce the liquid mixed binder into the reaction chamber.

22. In Paragraph 21, The above pump is A method for manufacturing a carbonation binder, wherein the above carbon dioxide is injected at a pressure greater than a preset pressure, and the above liquid mixed binder is provided with a venturi pump that applies pressure to the inside of the main body through the vacuum generated by the injection of carbon dioxide at a pressure greater than the preset pressure.

23. In Paragraph 20, The above main body is, A method for manufacturing a carbonation binder, comprising a static mixer section including a static mixer provided inside a passage to induce turbulent mixing for a liquid mixed binder discharged to a second discharge section connected to the other side, passing through a passage directly or indirectly connected to one side of the second input section and the carbon dioxide injection section.

24. In Paragraph 20, The above main body is, It includes a venturi tube section provided in the form of a venturi tube, and The second input section is connected to one side of the venturi tube, and The above second discharge section is connected to the other side of the above Venturi tube, and A method for manufacturing a carbonation binder, wherein the carbon dioxide injection part is provided such that the cross-section of the passage of the tube in the venturi tube is positioned closer to the position of the minimum cross-section between the position of the maximum cross-section and the position of the minimum cross-section.

25. In Paragraph 18, The second discharge unit is connected so that the liquid mixed binder discharged therefrom forms a spiral flow that proceeds spirally along the direction of gravity within the binder chamber, and A method for manufacturing a carbonation binder, wherein the inlet portion is connected to the binder chamber at a lower side than the second discharge portion to implement the circulation flow method.

26. In Paragraph 25, The binder chamber above It is provided in a cone shape with a diameter that decreases towards the bottom, and A method for manufacturing a carbonation binder, wherein the second discharge unit is connected to the interior of the binder chamber so as to discharge a liquid mixed binder that has reacted with carbon dioxide at least partially in the circumferential direction or tangential direction of the binder chamber.

27. In Paragraph 15, The above carbonation reaction device is, It further includes a temperature measuring device for measuring the temperature inside the binder chamber, and A method for manufacturing a carbonation binder, wherein the number of times the liquid mixed binder repeatedly passes through the reaction section is controlled based on the temperature measured by the temperature measuring device.

28. In Paragraph 15, The above carbonation reaction device is, It further includes a flow meter capable of measuring the amount of carbon dioxide injected by the carbon dioxide injection unit described above, A method for manufacturing a carbonation binder, wherein the number of times the liquid mixed binder repeatedly passes through the reaction section is controlled based on the amount of carbon dioxide injected measured through the flow meter.

29. In Paragraph 18, The above carbonation reaction device is provided in multiple units, and The above carbon dioxide buffer storage tank is configured to be shared with the plurality of carbonation reaction devices, and The first discharge portion of each of the plurality of carbonation reaction devices is connected, and A method for manufacturing a carbonation binder, wherein the plurality of carbonation reaction devices are provided in an alternating circulation method that alternately discharges the carbonation binder in the order in which the manufacturing of the carbonation binder is completed.

30. As a deep mixing treatment method for soft ground improvement, (a) a step of manufacturing a carbonation binder by a method for manufacturing a carbonation binder according to claim 1 or 15; (b) a step of preparing a carbonation mixture by stirring the carbonation binder with the original ground soil; and (c) A deep mixing treatment method for soft ground improvement comprising the step of curing the carbonation mixture to produce a soft ground improvement body.

31. A deep mixing treatment soft ground improved body using carbon dioxide, produced through the deep mixing treatment method for soft ground improvement pursuant to Paragraph 30.

32. A method for manufacturing concrete comprising a carbonate binder, wherein (a) a step of manufacturing a carbonation binder by a method for manufacturing a carbonation binder according to claim 1 or 15; and (b) A method for manufacturing concrete comprising the step of mixing the manufactured carbonation binder with aggregate to produce concrete.

33. A concrete member produced by a method for manufacturing concrete containing a carbonation binder according to paragraph 32.

34. As a carbonation reaction device, A binder chamber comprising a first input section into which a liquid mixed binder is introduced and a first discharge section for discharging at least a portion of the reacted liquid mixed binder; and A circulating transfer device comprising a reaction section connected to the binder chamber and in which the introduced liquid mixed binder reacts with carbon dioxide, wherein The above carbonation reaction device is provided to follow a circulating flow method in which the liquid mixed binder contained within the binder chamber repeatedly passes through the reaction section, and A carbonation reaction device in which carbon dioxide is supplied to the reaction section by a carbon dioxide injection section connected to the circulation transfer device.

35. As a carbon dioxide capture device, An absorbent chamber comprising a first input section into which a liquid carbon dioxide absorbent is introduced and a first discharge section for discharging at least a partially reacted liquid carbon dioxide absorbent; and A circulation transfer device comprising a reaction section connected to the absorber chamber and in which the introduced liquid carbon dioxide absorbent reacts with carbon dioxide of a carbon dioxide-containing gas, wherein The above carbon dioxide capture device is provided to follow a circulating flow method in which a liquid carbon dioxide absorbent contained within the absorbent chamber repeatedly passes through the reaction section, and A carbon dioxide capture device in which a carbon dioxide-containing gas is injected into the reaction section by a carbon dioxide-containing gas injection section connected to the circulation transfer device.

36. In Paragraph 35, A carbon dioxide capture device in which the above-mentioned carbon dioxide-containing gas is air or exhaust gas.

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