KR101871948B1 - Carbon dioxide conversion reactor, series reactors for carbon dioxide conversion and capture, and carbon dioxide conversion process using series reactors - Google Patents

Abstract

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a carbon dioxide conversion reactor, and more particularly, to a carbon dioxide conversion reactor which converts carbon dioxide contained in an exhaust gas into an aqueous bicarbonate solution that can be used for useful applications, And a carbon dioxide conversion reactor capable of remarkably reducing carbon dioxide in the flue gas with high efficiency and conversion speed, a series reactor for carbon dioxide conversion and collection including the same, and a carbon dioxide conversion process using the same.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a carbon dioxide conversion reactor, a carbon dioxide conversion reactor, a carbon dioxide conversion reactor, a carbon dioxide conversion reactor, a carbon dioxide conversion reactor,

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a carbon dioxide conversion reactor, and more particularly, to a carbon dioxide conversion reactor which converts carbon dioxide contained in an exhaust gas into an aqueous bicarbonate solution that can be used for useful applications, And a carbon dioxide conversion reactor capable of remarkably reducing carbon dioxide in the flue gas with high efficiency and conversion speed, a series reactor for carbon dioxide conversion and collection including the same, and a carbon dioxide conversion process using the same.

Carbon dioxide capture and storage technologies have been proposed as a method for reducing carbon dioxide, which is the cause of global warming. Carbon dioxide capture and storage technology refers to the technology of capturing carbon dioxide from sources such as power plants before leaving to the atmosphere, and then transporting them and storing them in a stable form. The carbon dioxide capture step consists of adsorption and desorption processes. First, in the adsorption process, carbon dioxide is collected from the exhaust gas using an absorbent capable of physically or chemically strong bonding with carbon dioxide. In the desorption process, external energy is applied to the absorbent bonding with carbon dioxide to regenerate the absorbent and extract only pure carbon dioxide. In order to stably reduce a large amount of carbon dioxide, it is preferable to use an absorbent that strongly binds to carbon dioxide, but there is a problem that energy consumed in the process of regenerating the absorbed carbon dioxide increases. In addition, the use of a sorbent having a weak binding force with carbon dioxide to lower the regenerated energy limits the efficiency of carbon dioxide reduction.

On the other hand, the captured carbon dioxide can be stored for permanent or semi-permanent isolation, for example, underground storage, ocean storage and surface storage. The underground storage can be easily isolated and stored, . The method of simple isolation and storage has been proposed to store in the waste oil field, gas field, and saline water (underground water layer over 800m underground), and EOR (Enhanced Oil Recovery) and ECBMR Enhanced Coal Bed Methane Recovery (COHM) recovery method) has been suggested. Such reutilization of carbon dioxide due to underground storage takes a long time, and there is a problem that drilling for underground storage is very expensive. In addition, the marine storage method is a method of releasing carbon dioxide into the ocean, and the carbon dioxide is stored in the form of hydrate by spraying at below 3000 m. However, marine storage is currently prohibited under international law due to the problems of degradation of ecosystem and stability of oceanic acidification. Furthermore, the surface storage method is a method in which carbon dioxide such as magnesium or potassium is chemically stored by reacting with additive minerals. However, this method has a secondary problem such as an excessive processing cost due to a slow speed and a cost for processing a material generated after the completion, and thus most of the researches have been made.

Recently, there have been proposed methods of converting carbon dioxide chemically and / or biologically, but the proposed methods have a problem of very low conversion efficiency, conversion amount, and conversion rate, and therefore, it is necessary to increase the residence time of the flue gas in the conversion process There is an unavoidable problem. In this case, the back pressure in the reactor is remarkably increased to make the conversion process itself unstable, and there is a problem of damage / breakage of the reactor.

Therefore, there is an urgent need to develop a carbon dioxide conversion method that can significantly improve the conversion speed of carbon dioxide, prevent an increase in back pressure due to exhaust gas supplied to the reactor, and exhibit a reduction effect due to the conversion of carbon dioxide .

Korean Patent Laid-Open Publication No. 2015-0006253

SUMMARY OF THE INVENTION The present invention has been made to solve the above problems, and it is an object of the present invention to convert carbon dioxide contained in an exhaust gas into a bicarbonate aqueous solution which can be utilized for useful applications, The present invention provides a carbon dioxide conversion reactor capable of reducing carbon dioxide in exhaust gas at a high efficiency and a conversion speed, and a carbon dioxide conversion process using the carbon dioxide conversion reactor.

In addition, the present invention provides a series reactor for carbon dioxide capture and conversion, which achieves the conversion and reduction of carbon dioxide through the carbon dioxide conversion reactor according to the present invention, while preventing the generation of back pressure and stably capturing and reducing carbon dioxide There is another purpose.

In order to solve the above-described problems, the present invention provides a gas purifier comprising: a gas supply unit to which an exhaust gas containing carbon dioxide is supplied; An enzyme reaction unit comprising a structure comprising a liquid filled in a part of the conversion reactor and a carbonic anhydrase for a reaction for converting the supplied carbon dioxide into bicarbonate ions; And a gas discharge unit for discharging the exhaust gas containing unreacted carbon dioxide to the outside in the enzyme reaction unit.

According to a preferred embodiment of the present invention, the apparatus may further include a bicarbonic acid aqueous solution discharge unit for discharging the bicarbonic acid aqueous solution converted and dissolved in the enzyme reaction unit.

According to another preferred embodiment of the present invention, the carbonic anhydrase may include at least one of wild type carbonic anhydrase and carbonic anhydrase variant. At this time, the wild-type carbonic anhydrase may include one or more selected from the group consisting of?,?,?,?,?, And recombinant carbonic anhydrase.

According to another preferred embodiment of the present invention, in order to prevent an increase in the back pressure of the reactor due to the exhaust gas supplied to the conversion reactor, a gas supply unit and a gas discharge unit are disposed above the interface between the liquid and the gas in the conversion reactor, The structure may be located at the interface to facilitate the conversion of carbon dioxide. At this time, a body part including the carbonic anhydrase and at least one float coupled to the body part and allowing the body part to be positioned at the interface may be further included. In addition, the carbonic anhydrase may be bound or received on the body part. In addition, the body part may include a channel for allowing the liquid and the carbon dioxide to contact with the carbonic anhydrase.

According to another preferred embodiment of the present invention, the carbonic anhydrase may be provided in any one or more of a plurality of uncoupled and aggregated enzyme aggregates and an enzyme cross-linking complex in which a plurality of enzymes are cross-linked.

According to another preferred embodiment of the present invention, the structure further comprises a body part, and the carbonic anhydrase further comprises a support and is bonded on the support or supported within the support, Lt; / RTI > The support may include at least one selected from the group consisting of polymer fibers, electrically conductive polymers, porous particles, spherical particles, nanoparticles, beads, carbon nanotubes, wires, pillars, graphene, have.

According to another preferred embodiment of the present invention, the enzyme cross-linking complex further comprises a first support comprising a first functional group on its surface, and the first carbonic anhydrase, which binds directly to the first functional group, And a second carbonic anhydrase crosslinking complex that binds to the first carbonic anhydrase and cross-links the adjacent carbonic anhydrase. The enzyme cross-linking complex may further comprise a second functional group on its surface, and the second functional group may be bonded to at least one of the first carbonic anhydrase and the second carbonic anhydrase cross-linking complex through the second functional group, And may further comprise a support.

According to another preferred embodiment of the present invention, it is possible to further include at least one of a bicarbonate aqueous solution reservoir and a bicarbonate aqueous solution reservoir to communicate with the bicarbonate aqueous solution discharge portion.

The present invention also relates to a gas supply unit for supplying an exhaust gas containing carbon dioxide; A carbon dioxide conversion unit including a liquid filled in a part of the conversion reactor to dissolve and convert the supplied carbon dioxide; And a gas discharge unit for discharging the exhaust gas containing unreacted carbon dioxide to the outside through the carbon dioxide conversion unit.

According to another aspect of the present invention, there is provided a carbon dioxide conversion reactor comprising: (1) supplying an exhaust gas to a gas supply unit of a carbon dioxide conversion reactor according to the present invention; And (2) some of the carbon dioxide contained in the supplied exhaust gas is converted to bicarbonate ions, and the exhaust gas containing unreacted remaining carbon dioxide provides a carbon dioxide conversion process that is discharged through the gas exhaust portion.

According to a preferred embodiment of the present invention, in the step (1), the flue gas is supplied from the upper portion of the liquid of the conversion reactor to prevent the increase of the back pressure of the reactor due to the flue gas supplied to the conversion reactor, The conversion reaction to bicarbonate ions can be promoted through the carbonic anhydrase provided in the structure located at the interface between the liquid and the gas inside the reactor.

The present invention also relates to a conversion reactor according to the invention; And a collection reactor communicating with the conversion reactor and collecting the introduced carbon dioxide, wherein the exhaust gas containing carbon dioxide is supplied to a conversion reactor or a collection reactor to convert or capture carbon dioxide, There is provided a series reactor for converting and collecting carbon dioxide which is introduced into a collection reactor or a conversion reactor to collect or convert the unreacted carbon dioxide.

According to a preferred embodiment of the present invention, the collection reactor may include a carbon dioxide absorbent or a carbon dioxide separation membrane.

According to another preferred embodiment of the present invention, the collection reactor includes a carbon dioxide collection discharge unit for discharging a collection including at least one of a carbon dioxide absorbent, a carbon dioxide intercalation compound and a reactive compound, And a carbon dioxide desorbing unit for separating and collecting carbon dioxide from the collected exhausted water.

Hereinafter, terms used in the present invention will be described.

The meaning of "on A phase" used in the present invention is meant to include both the surface of A directly or indirectly through B.

The carbon dioxide conversion reactor according to the present invention can convert the carbon dioxide contained in the flue gas into a useful by-product, and at the same time enables a rapid conversion process to prevent an increase in the back pressure due to the supplied flue gas, It is possible to remarkably reduce the carbon dioxide in the flue gas. In addition, the present invention can be applied to a series reactor capable of achieving conversion and reduction of carbon dioxide through the carbon dioxide conversion reactor and preventing the generation of back pressure, thereby stably capturing and reducing carbon dioxide. And can be applied to various industries that can generate high added value.

1 is a schematic view of a carbon dioxide conversion reactor according to a preferred embodiment of the present invention.
2 and 3 are cross-sectional schematic views of a carbonic anhydrase aggregate included in a preferred embodiment of the present invention.
4 is a schematic plan view of a structure having a carbonic anhydrase complex included in a preferred embodiment of the present invention.
5 is an exploded perspective view of a structure included in a preferred embodiment of the present invention.
FIG. 6 and FIG. 7 are schematic views of a series reactor showing a process for converting and collecting carbon dioxide when the supply direction of the exhaust gas containing carbon dioxide is changed for a serial reactor according to a preferred embodiment of the present invention.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings, which will be readily apparent to those skilled in the art to which the present invention pertains. The present invention may be embodied in many different forms and is not limited to the embodiments described herein. In order to clearly illustrate the present invention, parts not related to the description are omitted, and the same reference numerals are assigned to the same or similar components throughout the specification.

The carbon dioxide conversion reactor 101 according to an embodiment of the present invention is configured such that carbon dioxide supplied as shown in FIG. 1 stays and the interior of the carbon dioxide conversion reactor 101 is filled with an empty reaction chamber 151, A gas supply unit 111 disposed at one side of the reaction chamber 151 to supply an exhaust gas containing carbon dioxide to the inside of the reaction chamber 151, an enzyme reaction unit 121 for converting carbon dioxide into bicarbonate ions, A bicarbonate aqueous solution discharge unit 131 for discharging the converted bicarbonate ions to the outside, and a gas discharge unit 141 for discharging an exhaust gas containing unreacted carbon dioxide from the enzyme reaction unit 121 to the outside, And a bicarbonate aqueous solution reservoir (301) directly connected to the bicarbonate aqueous solution discharge unit (131). The conversion reactor 101 serves to convert the high concentration of carbon dioxide contained in the exhaust gas into bicarbonate ions. Such a carbon dioxide conversion process is more environmentally friendly than other methods of reducing and / or converting carbon dioxide, Can be converted into usable bicarbonate ions to create added value, which is very advantageous in terms of economy and productivity. In addition, since carbonic anhydrase can theoretically convert one million carbon dioxide molecules per second into bicarbonate ion, it is very suitable for the conversion of carbon dioxide which flows at a high rate, thereby preventing further increase of the back pressure in the reactor And there is an advantage in that it does not require additional processes such as desorption of captured carbon dioxide separated from the exhaust gas.

The exhaust gas discharged from the carbon dioxide generating source, such as a thermal power plant, is supplied to the gas supply unit 111 of the conversion reactor 101, do. At this time, the gas supply unit 111 may be disposed above the interface between the liquid 121b and the gas inside the switching reactor 101. [ The flue gas containing carbon dioxide supplied through the flue gas is supplied from the upper part of the liquid 121b without passing through the liquid 121b of the enzyme reaction unit 121, And may have a fluid flow that is discharged to the upper portion of the liquid 121b and the gas discharge portion 141 located above the liquid. When the gas supply unit 111 and the gas discharge unit 141 are disposed in consideration of the height of the liquid 121b in the reaction chamber 151 so as to have such a fluid flow, the exhaust gas to be supplied can flow and pass through the inside of the reactor more smoothly. There is an advantage that the increase of the back pressure caused by the resistance of the flue gas flow generated while passing through the liquid can be remarkably reduced.

Next, the carbon dioxide contained in the exhaust gas supplied to the gas supply unit 111 is converted into bicarbonate ions through the structure 121a including the carbonic anhydrase aggregate contained in the enzyme reaction unit 121 and the liquid 121b. And it can have a carbon dioxide reducing effect.

The liquid 121b may be used without limitation in the case of a solvent (or a solution) which functions as a reaction medium and / or a reaction material for converting carbon dioxide into bicarbonate ions and has no problem in dissolving bicarbonate ions to be converted. By way of non-limiting example, the solvent (or solution) may be water and / or a conventional buffer solution, and as a non-limiting example of the buffer solution, 2-amino-2-hydroxymethyl- Propanediol can be used.

The structure 121a includes a carbonic anhydrase which promotes the conversion of carbon dioxide to bicarbonate. The structure 121a may include a carbonic anhydrase and may be disposed in a part of the interior of the liquid 121b or may be uniformly dispersed therein. However, in order to reduce the back pressure, when the position of the gas supply unit is disposed above the liquid 121b and the exhaust gas is supplied from above the liquid, the structure body 121a may be formed of a liquid And at the interface of the gas.

The above-mentioned carbonic anhydrase can be used without limitation as long as it is a known enzyme having a function of promoting the conversion of carbon dioxide to bicarbonate ion. For example, among the wild type carbonic anhydrase and carbonic anhydrase mutant And may include any one or more of them. At this time, the wild-type carbonic anhydrase may be an enzyme naturally existing in vivo in an animal, a plant, or the like, and therefore it may be one or more selected from the group consisting of?,?,?,? And / or in vivo, or by artificially recombining the enzyme, or in combination with the in vivo carbonic anhydrase. The artificially recombined carbonic anhydrase may be a known one, and the amino acid sequence thereof is not particularly limited in the present invention. The carbonic anhydrase mutant is a modification of a part or all of the amino acid sequence of a carbonic anhydrase which exists naturally, and has a basic function of carbonic anhydrase and naturally occurring carbonic anhydrase The amino acid sequence is not particularly limited in the present invention.

The above-mentioned carbonic anhydrase may be contained in any one or more of a free enzyme dispersed on a structure, an enzyme aggregate in which a plurality of non-aggregated aggregates are aggregated, and an enzyme cross-linked complex in which a plurality of aggregates are mutually combined.

In addition, the carbonic anhydrase may be included in the structure with the support or may be included in the structure without the support.

First, a case where a support is provided will be described. The carbonic anhydrase may be bound on the support or supported on the support.

The support serves to bind or support a carbonic anhydrase, to serve as a base for integrating carbonic anhydrase, and to protect the carbonic anhydrase from external force. In addition, when the carbonic anhydrase is in the form of an aggregate or a cross-linked complex, it can function to distribute and distribute the whole structure to the structure while stably maintaining the form. There is no particular limitation on the shape of the support, as long as it does not inhibit or inhibit the activity of the enzyme, and is not limited to beads, fibers, or plates. For example, the support may be any one or more selected from the group consisting of polymer fibers, electrically conductive polymers, porous particles, spherical particles, nanoparticles, beads, carbon nanotubes, wires, pillars, graphene, have. Furthermore, the size of the reactor can be designed differently according to the specific structure and shape of the conversion reactor, so that the present invention does not particularly limit it.

When the above-mentioned carbonic anhydrase is bound on a support, the bond is formed by physical bonding (e.g., adsorption) of carbonic anhydrase and / or chemical bonding of carbonic anhydrase through a specific functional group provided on the support Ionic bonding, covalent bonding, etc.). It may also be applied on a support by an adhesive material adhesive material based on catechol groups, such as polydopamine, polynorepinephrine. In the case where the support has a porous structure, the support may be provided with a carbonic anhydrase in the pores or cavities contained therein, and may be formed by forming an aggregate or a cross-linked complex. The supported carbonic anhydrase may be bound to the inner surface of the pores or the cavity of the cavity or may be accommodated in a non-bonded state, but the present invention is not limited thereto.

On the other hand, there may be a difference between an optimum condition in which the reaction for converting carbon dioxide into bicarbonate ion occurs optimally and an optimum condition for maintaining the enzyme activity of carbonic anhydrase, and in some cases, the environment in the conversion reactor is a carbonic anhydrase Enzyme activity may be difficult to maintain. As shown in FIG. 2, the enzyme cross-linking complex 1000 may include a first support (1001) having a first functional group (1001) on the surface thereof, 1010) to bind to the first carbonic anhydrase 1100 and the first carbonic anhydrase 1100 fixed to the first functional group 1001 and to bind a plurality of carbonic anhydrase cross-linked 1212, 1212, and 1213 of the second carbonic anhydrase cross-linking complexes 1210, 1211, 1212, and 1213.

The functional group (1001) provided on the surface of the support (1010) may be used without limitation in the case of a functional group capable of fixing the first carbonic anhydride enzyme (1100). For example, a functional group such as carboxyl group, amine group, imine group, An ether group, an acetal group, a sulfide group, a phosphate group, and an iodo group, preferably a carboxyl group and / or an alkyl group, Or an amine group.

When the carbonic anhydrase forms a carbonic anhydrase crosslinking complex (1000) having a structure as shown in FIG. 2, the enzyme activity is excellent even at the temperature and pH conditions which may be unsuitable for maintenance / expression of carbonic anhydrase activity There is an advantage that the period can be stably expressed.

The carbonic anhydrase crosslinking complex (1000) as shown in FIG. 2 can be prepared by the same method as that of Example 1 described below. In this case, only the crosslinking agent is added without introducing the precipitating agent, An enzyme crosslinking complex can be prepared. However, when a precipitating agent is added, a carbonic anhydrase crosslinking complex in which a carbonic anhydrase is accumulated more densely can be prepared. However, the production method of the carbonic anhydrase crosslinking complex as shown in FIG. 2 is not limited to the example 1, and Korean patent application publication Nos. 10-2011-0128182, 10-2011-0128134 No. 10-2013-0127916, and the like can be incorporated by reference.

On the other hand, in order to express more excellent enzyme activity and to express the activity stably for a long period of time, a large amount of enzyme bound to the complex is required, and at the same time, an excellent binding force capable of preventing the enzyme from falling off by the external force is required.

3, the carbonic anhydrase crosslinking complex 2000 may include a first support 2010 having a first functional group 2001 on its surface, a second functional group 2301 on the surface thereof, , 2302), wherein the second support (2300)

The first carbonic anhydrase 2100 and the second carbonic anhydrase crosslinking complexes 2211, 2212 and 2213 can be bonded to the second support body 2300 through the second functional group.

The second carbonic anhydrase cross-linking complex is not crosslinked only between the enzymes but can be bound between the enzymes with a stronger binding force as they are covalently bound through the second support, and the second support bodies 2300 Since this enzyme can be a binding point to be covalently bonded in a cluster, a larger amount of the enzyme can be included in the complex and can be advantageously used for expressing the enzyme activity remarkably improved and the enzyme activity stably for a long time have. The second support body 2300 is the same as the above description of the support body (first support body). The first support body may be the same as or different from the second support body, and may have the same shape or size as the second support body This is not particularly limited in the present invention. The second functional group is also the same as the functional group described above, and the first functional group may be the same as or different from the second functional group. 3, the second support body 2300 may be a magnetic support. In this case, the liquid 120b, in which the bicarbonate ions converted in the conversion reactor 100 are dissolved, is discharged through the bicarbonate ion discharge unit 131 It is possible to prevent the release of the carbonic anhydrase complex by using magnetism at the time of discharging or to enable the separation and recycling of the carbonic anhydrase complex contained in the discharged liquid.

The carbonic anhydrase crosslinking complex 2000 according to FIG. 3 can be prepared by the manufacturing method according to Example 2 described later. However, as in the case of the carbonic anhydrase complex according to FIG. 3, only the introduction of the crosslinking agent 3 can also be realized. However, it is possible to realize a complex in which a higher concentration of the enzyme is integrated by introducing the precipitating agent, and thereby, the improved physical properties can be exhibited. The method for producing the carbonic anhydrase crosslinking complex as shown in FIG. 3 is not limited to the example 2, and Korean Patent Laid-Open Nos. 10-2011-0128182, 10-2011-0128134, 10-2013-0127916 and the like can be inserted by reference.

The above-mentioned carbonic anhydrase on the support or on the support may be provided in the enzyme reaction part through binding or acceptance of the support on the construct. At this time, the bonding may be a physical and / or chemical bonding or a bonding via an adhesive material, and the present invention is not particularly limited thereto.

In addition, the carbonic anhydrase may be provided in a structure without a support, and the carbonic anhydrase may be included on the body when the construct described below includes a body part. The binding can be fixed through chemical bonding (e.g., ionic bonding, covalent bonding, etc.) of carbonic anhydrase via physical binding (e.g., adsorption) of carbonic anhydrase and / or specific functional groups provided on the body part have. It may also be adhered to the body portion by an adhesive substance adhesive material based on catechol groups, such as polydopamine, polynorepinephrine. In the case where the body part is porous, the support may be provided with a carbonic anhydrase in the pores or cavities contained therein, and may be formed by forming an aggregate or a cross-linked complex. The supported carbonic anhydrase may be bound to the inner surface of the pore or the cavity of the cavity or may be accommodated in a non-bonded state, but the present invention is not limited thereto.

On the other hand, considering the amount of the supplied flue gas and the fast feeding speed, the fluid flow supplied from the upper part of the interface of the liquid 121b in the reaction chamber 151 and discharged and discharged further shortens the flue gas retention time in the reaction chamber 151 There may be a problem in that the residence time required to convert the carbon dioxide contained in the flue gas to the desired level may not be ensured. That is, when the flow of the flue gas passing through the liquid 121b is formed inside the switching reactor 101, the back pressure may be generated and increased due to the fluid resistance flowing in the liquid, To the upper part of the interface of the liquid 121b may be advantageous from the viewpoint of preventing the back pressure increase. However, in this case, the supplied carbon dioxide is inevitably confined to the liquid interface in which the part where the conversion reaction occurs is in contact with the enzyme reaction part, The residence time in the reactor is very short. Accordingly, if the carbonic anhydrase aggregate that promotes the conversion of carbon dioxide is located at a lower portion of the reaction chamber 151 away from the interface of the liquid or uniformly dispersed in the entire liquid, carbon dioxide in the exhaust gas passing through the reactor rapidly reaches a desired level It may be difficult to convert. Also, if the residence time of the flue gas is increased to solve this problem, the back pressure in the conversion reactor may increase.

According to a preferred embodiment of the present invention, the structure 121a including the carbonic anhydrase can be disposed on the liquid-gas interface as shown in FIG. 1, and through this, the carbonic anhydrase can be more actively converted The reaction can be promoted, and ultimately, the increase of the carbon dioxide conversion rate, the increase of the carbon dioxide reduction efficiency, and the occurrence or increase of the back pressure can be minimized or prevented.

The structure 121a may be fixed to the side of the reaction chamber 151 at the interface height so that the structure 121a is positioned at the interface between the liquid 121b and the gas. It is preferable that the structure 121a is designed to float on the liquid because there is a difficulty in keeping the height constant at all times.

4, the structure 1 includes a body 10 including a carbonic anhydrase crosslinking complex 1000 and a body 10 coupled to the body 10, And at least one floating portion 31,35 for floating on the liquid 121b.

5, the first body 11 and the second body 21 are arranged in parallel with each other in the vertical direction, and each of the first body 11 and the second body 21 may be a planar structure in the form of a lattice.

At this time, the second body 21 may be disposed adjacent to the surface of the liquid. For example, the second body 21 may be immersed in the liquid or floating on the liquid surface.

In FIG. 5, the first body 11 and the second body 21 are separated into a single structure and are arranged in parallel with each other. However, the first body 11 and the second body 21 may be integrally formed.

In an embodiment of the present invention, protrusions 15 and 25 may be formed at both ends of the body 10 to be coupled to the floating units 31 and 35. However, the protrusions 15 and 25 of the body 10 may be inserted into the coupling grooves 33a and 37b of the floating portions 31 and 35, but the present invention is not limited thereto.

At this time, the body portion 10, that is, the first body 11 and the second body 21 may be formed of acrylonitrile-butadiene-styrene, polythiophene, polylactic acid, polyvinyl alcohol, polycaprolactam, poly Polypropylene oxide, polyurethane, polyglycolic acid, polyethylene terephthalate, polymethylmethacrylate, polystyrene, polydimethylsiloxane, polydimethylsiloxane, polyvinylpyrrolidone, polyvinylpyrrolidone, caprolactone, polylactic-co-glycolic acid, polyacrylonitrile, polyester, polyethylene, polyethyleneimine, , Carbonic anhydrase crosslinking complex (1000) formed by at least one of polystyrene-co-maleic anhydride, teflon, collagen, nylon, cellulose, chitosan, glass, gold, silver, aluminum, iron, And can be directly coupled to the first body and the second body.

The first auxiliary fluid 31 of the floating units 31 and 35 may be coupled to the left end of the main body 10 with reference to FIG. May be coupled to the right end of the body portion with reference to the other end portion of the body portion, for example, Fig.

Meanwhile, as shown in FIG. 5, in the embodiment of the present invention, the first and third sub-fluids 31 and 35 may be formed in a rectangular parallelepiped shape so that air can be filled therein. Whereby the structure 1 according to an embodiment of the present invention can be suspended on the liquid.

However, in an embodiment of the present invention, the first sub-fluid 31 and the second sub-fluid 35 may be formed in any form if they are made of a material that can be placed on the liquid.

Referring to FIG. 5, the protrusions 33 and 37 may be formed in a rectangular parallelepiped shape in each of the first fluid 31 and the second fluid 35 in an embodiment of the present invention.

At this time, the projections 33 and 37 are formed on the left side where the first fluid 31 is coupled to the body 10, for example, the right side or the second fluid 35 is coupled to the body 10 .

5, the protrusions 33 and 37 may be formed with coupling grooves 33a and 37b into which the protrusions 15 and 25 of the body 10 are inserted and fitted. At this time, the coupling grooves 33a and 37b may be formed so as to correspond to the protrusions so as to be fitted to the protrusions 15 and 25. [

Meanwhile, in one embodiment of the present invention, the first fluid 31 and the second fluid 35 are selected from the group consisting of acrylonitrile-butadiene-styrene, polythiophene, polylactic acid, polyvinyl alcohol, polycaprolactam , Polycaprolactone, polylactic-co-glycolic acid, polyacrylonitrile, polyester, polyethylene, polyethyleneimine, polypropylene oxide, polyurethane, polyglycolic acid, polyethylene terephthalate, polymethylmethacrylate, polystyrene, poly At least one of dimethylsiloxane, polystyrene-co-maleic anhydride, Teflon, collagen, nylon, cellulose, chitosan, glass, gold, silver, aluminum, iron, copper and silicon.

The carbonic anhydrase crosslinking complex 1000 may be accommodated between the first and second bodies 11 and 21 constituting the body 10 as shown in FIGS. Lt; / RTI > At this time, the bonding is carried out by bonding the body part 10 to the body part 10 through adhesion using an adhesive material, physical bonding (e.g., adsorption) and / or chemical bonding (e.g., ionic bonding, covalent bonding, etc.) ) Or may only be physically received in a non-bonded state. In addition, the portion of the carbonic anhydrase crosslinking complex 1000 to be coupled to the body 10 may be a carbonic anhydrase and / or a support.

In addition, the body 10 may include a channel for allowing carbon dioxide and liquid to flow into the carbonic anhydrase complex 1000 so as to be in contact therewith. For example, as shown in FIGS. 4 and 5, A plurality of channels in the lattice can be formed.

1, the conversion reactor 101 can discharge the aqueous bicarbonic acid solution having the converted bicarbonate ions dissolved therein through the aqueous bicarbonate aqueous solution discharge unit 131. The discharged bicarbonate ions are discharged to the bicarbonate aqueous solution discharge unit 131 In a bicarbonate aqueous solution reservoir 301 which is in communication with the bicarbonate aqueous solution discharging portion 131 and / or in a separate bicarbonate aqueous solution reservoir 301 communicated with the bicarbonate aqueous solution discharging portion 131. The bicarbonate aqueous solution buffer may be formed by synthesizing bicarbonate ions converted and / or collected as carbonates, culturing them as a raw material, removing metal cations, purifying radioactive materials, and the like.

In addition, the present invention can also be formed with a liquid filled in a part of the conversion reactor for the reaction to convert the carbon dioxide supplied to the bicarbonate ion, unlike in Fig.

A method for converting carbon dioxide through the conversion reactor according to one preferred embodiment of the present invention will now be described. The method comprises: supplying an exhaust gas to a gas supply unit 111 of a carbon dioxide conversion reactor 101; And (2) a portion of the carbon dioxide contained in the supplied exhaust gas is converted into bicarbonate ion through a liquid or enzyme reactor 121 filled in a part of the conversion reactor, and the exhaust gas containing unreacted carbon dioxide is converted into a gas discharge portion 141, Lt; / RTI >

The detailed description of the steps (1) and (2) is the same as that of the above-described conversion reactor, and thus will not be described. The step (2) in the conversion reactor may preferably be carried out at a pH of 7.5 to 8.5 and a temperature of 25 to 45 ° C.

In the step (1), the flue gas is supplied from the upper portion of the liquid in the conversion reactor to prevent the back pressure of the reactor from increasing due to the flue gas supplied to the conversion reactor. The carbon dioxide in the supplied flue gas, The conversion reaction to bicarbonate ion can be promoted through the carbonic anhydrase enzyme provided in the structure located at the center of the cell.

In the meantime, the present invention includes a series reactor for converting and collecting carbon dioxide, which is implemented by including the above-described conversion reactor, and the above-mentioned series reactor has a collecting reactor, thereby achieving a further enhanced carbon dioxide reduction efficiency and an effect of suppressing an increase in back pressure have.

6 and 7, a series reactor for converting and collecting carbon dioxide according to an embodiment of the present invention includes a conversion reactor 101 and a collection reactor 201 communicated with each other so that carbon dioxide can flow from one side to the other, , And a carbon dioxide desorber (401) for separating and collecting the carbon dioxide collected in the collection reactor (201) and a bicarbonate aqueous solution reservoir (301) for collecting the bicarbonate ions converted through the conversion reactor can do.

In the series reactor having a carbon dioxide gas flow as shown in FIG. 6, the exhaust gas containing carbon dioxide is supplied to the conversion reactor 101 through the gas supply unit 111 After the carbon dioxide is converted through the liquid or enzyme reaction unit 121, the exhaust gas containing unreacted carbon dioxide is supplied to the collection reactor 201 through the gas discharge unit 141 of the conversion reactor 101, The carbon dioxide is collected and the exhaust gas containing carbon dioxide not collected in the collecting process can be discharged through the gas discharging unit 221 of the collecting reactor 201.

7, carbon dioxide is collected after the exhaust gas containing carbon dioxide is supplied through the gas supply unit 221 of the collection reactor 201, and the uncoated carbon dioxide is supplied to the gas supply unit The carbon dioxide is converted through the enzyme reaction unit 121 and the unreacted carbon dioxide is supplied to the conversion reactor 101 via the gas discharge unit 111 of the conversion reactor 101 Can be discharged.

6 and 7 are compared with conventional carbon dioxide abatement devices or switching devices, the rapid flow rate of the supplied exhaust gas and thus the backpressure of the reactor, the carbon dioxide conversion / collection ability of the reactor itself It is possible to considerably reduce the back pressure applied to the reactor and to reduce the conversion efficiency of the carbon dioxide and the conversion efficiency A further enhanced effect can be obtained.

In particular, the conventional carbon dioxide abatement apparatus reduces carbon dioxide by using an absorber or a separator. The absorber or separator requires a certain time for collecting carbon dioxide in the flue gas due to its efficiency. In addition, There is a problem in that satisfactory efficiency can not be exhibited in separating the gases such as carbon dioxide and other gases from each other on the development level. Accordingly, in order to collect the entire amount of carbon dioxide contained in the flue gas, it is required not only to use an absorbent or separation membrane having a high collection efficiency but also to keep the flue gas in the reactor for a predetermined time or more. However, considering the amount of exhaust gas discharged from a thermal power plant or the like and the high flow rate, the exhaust gas flowing into the reactor having a limited volume and a limited collection efficiency is difficult to secure the residence time in the reactor to the extent necessary for capturing the entire amount of carbon dioxide, The flue gas discharged through the reactor without being allowed to stay in the reactor may contain a large amount of unoccupied carbon dioxide, so that the efficiency of reducing carbon dioxide may not be good.

In order to solve this problem, when a sorbent having a high collection efficiency is used, a great amount of energy is consumed in the separation process of collected carbon dioxide, and there may be a problem that carbon dioxide is generated / discharged for the production of such energy. Also, if the residence time of the carbon dioxide in the reactor is sufficiently secured by another method, the carbon dioxide capture efficiency can be increased. However, considering the amount and flow rate of the exhaust gas discharged very rapidly, the increase of the back pressure in the reactor, Destabilization of the reactor and damage / breakage of the reactor.

Accordingly, the present invention can be achieved by connecting the conversion reactor 101 and the collecting reactor 201 according to the present invention in series, and supplying the exhaust gas to the collection reactor 201 or the conversion reactor 201 via the conversion reactor 101 or the collection reactor 201. [ It is possible not only to remarkably improve the efficiency of reducing carbon dioxide, but also to obtain a reflex effect that can prolong the residence time of the flue gas staying in the entire series reactor, It is possible to achieve the target conversion / reduction efficiency and the increase in the back pressure of the reactor at the same time, and the process load caused by having any one of them can be prevented.

Furthermore, the reduction of the process load may be free from the restriction that the carbon dioxide conversion power of the carbonic anhydrase used in the carbon dioxide conversion and / or the capture process and / or the trapping power of the carbon dioxide sorbent should meet a certain level or more, It is very advantageous in terms of cost reduction.

In addition, the conversion process of the carbon dioxide through the conversion reactor 101 can produce not only the reduction of carbon dioxide in the flue gas but also the byproducts that can be utilized for various sale of the flue gas, so that the economic benefit of preventing environmental pollution and creating added value can be obtained at the same time.

When carbon dioxide is reduced through the conversion reactor 101 and the unreacted carbon dioxide is collected as shown in FIG. 6, carbon dioxide in the exhaust gas is primarily reduced through the conversion reactor 101, 201) can maintain a high level of carbon dioxide abatement efficiency because only a very low concentration of carbon dioxide is contained in the exhaust gas discharged through the series reactor even though an absorbent having a weak bonding force with carbon dioxide is used, and the carbon dioxide bonded to the weak absorbent is separated As less energy is consumed, there is less concern about the generation of energy for separating carbon dioxide and thus the additional emission of carbon dioxide. In contrast, the series reactor shown in FIG. 6 can achieve the desired level of conversion and reduction of carbon dioxide even when the collection efficiency in the collection reactor is relatively low as compared with the series reactor shown in FIG. 7, As energy can be consumed, it can be advantageous in terms of economy and environment.

When a plurality of collecting reactors are connected in series, it is possible to prevent the back pressure from occurring, but the energy required for separating the collected carbon dioxide is increased by that much And there is a problem that the generation and emission of carbon dioxide are further increased due to the increased energy production. In addition, as described later, there is a problem in that it is not possible to simultaneously produce useful by-products during the reduction process through the capture of carbon dioxide, which is disadvantageous to economic benefits through creation of added value. In addition, if several conversion reactors are connected in series, the number of conversion reactors to be provided can be remarkably increased considering the reduction efficiency of carbon dioxide through the conversion reactor, . In addition, when the conversion reaction of carbon dioxide is a reversible reaction, the limitation on the carbon dioxide reduction efficiency is clear.

On the other hand, it can be considered to cause the carbon dioxide capture reaction and the conversion reaction to occur in one reactor simultaneously to achieve reduction of equipment and conversion / collection. For example, in one reactor, carbon dioxide absorbent and carbonic anhydrase However, since most of the absorbent solution has a temperature of 40 to 60 ° C and a pH of about 9 to 12 at a high temperature and a strong alkaline environment, the carbonic anhydrase is a very harsh environment for maintaining long-term activity, The enzyme activity can not be stably maintained for a long period of time and frequent enzyme replacement is required, which may lead to an increase in conversion cost. Even if carbonic anhydrase is provided at the same time, since the carbon dioxide in the flue gas is very concentrated, the amount of carbon dioxide discharged as the flue gas increases and the amount of carbon dioxide in the flue gas is reduced It can be difficult.

Each constitution of the series reactor based on the flow of the exhaust gas as shown in Fig. 6 will be described below.

The exhaust gas containing carbon dioxide is first supplied to the conversion reactor 101 to convert carbon dioxide into bicarbonate ions, thereby reducing carbon dioxide at the same time as production of useful by-products. The description of the conversion reactor 101 is the same as that described above and is omitted. The flue gas containing unreacted carbon dioxide in the liquid or enzyme reaction section 121 of the conversion reactor 101 may be supplied to the collection reactor 201 through the gas discharge section 141.

Next, the collection reactor 201 connected in series with the above-described conversion reactor 101 will be described.

The collection reactor 201 plays a role of collecting unreacted carbon dioxide in the conversion reactor 101. When the exhaust gas containing carbon dioxide is supplied into the reaction chamber 231 of the collection reactor 201 through the gas discharge unit 141 of the conversion reactor 101, the supplied carbon dioxide is collected in the reactor, The exhaust gas containing carbon dioxide can be discharged to the outside through the gas discharge unit 221 of the collection reactor 201 thereafter. The collection reactor 201 can separate and collect carbon dioxide through a carbon dioxide separation membrane and / or carbon dioxide through an absorbent.

Since the carbon dioxide separation membrane may be a conventional carbon dioxide separation membrane, the carbon dioxide separation membrane known in the art may be used without limitation in specific materials and structures. As a non-limiting example, the material of the carbon dioxide separation membrane may be 6FDA polyimide, Cardo-type polyimide, polysulfone, cellulose acetate or the like, which is excellent in separation characteristics of CO ₂ / N ₂ as an organic polymer. In addition, the specific structure may be a structure including a porous inorganic film coated on porous steel or a ceramic support, or a polymer membrane structure having a glass-like polymer or a rubber-like polymer having a permeability selectivity. In the mechanism, if the separation membrane is the porous inorganic membrane, it may be classified into Knudsen diffusion according to molecular weight, surface diffusion due to surface attraction, capillary condensation, molecular sieve mechanism depending on the size of molecules, but not limited thereto. Accordingly, it is possible to select and use an appropriate separation membrane.

The carbon dioxide absorbent may be a conventional carbon dioxide absorbent, and may specifically include at least one of a dry absorbent and a wet absorbent. The dry absorbent may, for example, include solid amines, alkali metal salts, alkaline earth metal salts, zeolites, metal organic structures and the like. The wetting agent may be a conventional wetting agent, preferably an amine-based aqueous solution, and may be a monoethanolamine, diethanolamine, dimethylethanolamine, diethylethanolamine, dimethylglycine, N-methyldiethanolamine Amino-2-hydroxymethyl-1, 3-propanediol, piperidine, pyperazine, potassium carbonate, sodium carbonate, ammonia and ammonium carbonate And may include any one selected.

According to a preferred embodiment of the present invention, the collection reactor may further include a carbonic anhydrase cross-linking complex when it comprises a carbon dioxide absorbent, preferably a wet absorbent. When the carbonic anhydrase crosslinking complex is further included in the collection reactor, the collection efficiency of carbon dioxide can be further improved and the collection rate can be further increased. However, the carbon dioxide capture environment of the capture reactor may be an alkaline pH of 9 to 12 and a temperature of 40 to 60 ° C. Under such conditions, denaturation of the carbonic anhydrase may occur and the activity of the enzyme may be significantly lowered . Therefore, in order to stably and excellently express the enzymatic activity for a long period of time, the carbonic anhydrase may be different from the carbonic anhydrase contained in the conversion reactor, and preferably, the carbonic anhydrase is cross- And an integrated carbonic anhydrase crosslinking complex may be advantageous.

The carbon dioxide adsorbent collected through the collection reactor 201 and the carbon dioxide supplied from the above-described conversion reactor 101 and the carbon dioxide-containing conjugate and the above-mentioned collected product containing the reactive compound are discharged through the collected- The remaining amount of the exhaust gas excluding the carbon dioxide captured in the exhaust gas containing carbon dioxide supplied from the conversion reactor 101 is supplied to the carbon dioxide desorber 401 for separating and collecting the carbon dioxide, Or may be re-supplied to the gas supply unit 111 of the conversion reactor 101 to repeat the carbon dioxide reduction process.

The desorber 401 may include a chamber 421 for storing the supplied collected material and separated carbon dioxide, an energy supply unit 411 for generating energy, for example, heat in the carbon dioxide separation process, And a carbon dioxide discharging unit 431 for discharging the carbon dioxide. The heat applied at this time may be 40 to 60 ° C, but is not limited thereto and may be changed depending on the type of the absorbent of carbon dioxide used.

6 and FIG. 7, the gas supplier 111 in the switching reactor 101 is operated as shown in FIG. 7 to generate a different flue gas flow through the same series reactor, And the trapping reactor 201 may also be implemented by employing methods and configurations known in the art such that the gas discharge portion 221 in Figure 6 functions as the gas supply portion 221 in Figure 7. [ have. Alternatively, unlike in FIGS. 6 and 7, each of the conversion reactor and the collecting reactor may include a gas supply unit into which the exhaust gas can directly flow, and each gas supply unit may be implemented as an opening and closing type, So that the carbon dioxide conversion and collection process can be performed. That is, the reactor in which the flue gas flows first may be selected in consideration of the amount of the supplied flue gas, the concentration of carbon dioxide, and the required degree of bicarbonate ion. At this time, the flue gas directly flows into the selected reactor, The gas supply may be closed to prevent direct entry of the flue gas. The opening or closing of the gas supply unit may be changed in consideration of the amount of the exhaust gas remaining in the reactor even during the process of converting and collecting the exhaust gas after the exhaust gas is supplied to the series reactor.

As described above, the carbon dioxide contained in the exhaust gas through the series reactor according to the present invention can be directly converted into the carbon monoxide gas in the case where the exhaust gas is directly supplied to the conversion reactor as shown in FIG. 6: (i) Converting the carbon dioxide into bicarbonate ions; And (ii) supplying an exhaust gas containing unreacted carbon dioxide in the supplied carbon dioxide to a collection reactor to collect carbon dioxide, whereby carbon dioxide can be converted and collected.

 When the exhaust gas is directly supplied to the collection reactor as shown in FIG. 7, (a) an exhaust gas containing carbon dioxide is supplied to a collection reactor of a tandem reactor according to an embodiment of the present invention to collect the carbon dioxide; And (b) supplying an exhaust gas containing uncoated carbon dioxide in the supplied carbon dioxide to a conversion reactor to convert the carbon dioxide to bicarbonate ions, whereby carbon dioxide can be converted and collected.

The conversion and collection of carbon dioxide will be described with reference to a series reactor as shown in FIG. 6, and the detailed description of the step (i) will be omitted since it is the same as that described in the above-mentioned conversion reactor. It may be more advantageous to carry out the carbon dioxide conversion process in the conversion reactor, preferably at a pH of 7.5 to 8.5 and a temperature of 25 to 45 < 0 > C.

In the step (i), the flue gas is supplied from the upper portion of the liquid in the conversion reactor in order to prevent the increase of the back pressure of the reactor due to the flue gas supplied to the conversion reactor. The carbon dioxide in the supplied flue gas, The conversion reaction to bicarbonate ion can be promoted through the carbonic anhydrase enzyme provided in the structure located at the center of the cell.

Further, the detailed description of the step (ii) is the same as the description in the above-described collecting reactor and is omitted. The carbon dioxide capture step in the collection reactor is preferably carried out at a pH of 9 to 12 and a temperature of 40 to 60 ° C, preferably 45 to 55 ° C. If the temperature is lower than 40 ° C., the carbon dioxide can not be reduced to the desired level. If the temperature is higher than 60 ° C., the solubility of carbon dioxide is lowered and the amount of carbon dioxide discharged into the gaseous state is significantly increased. There is a problem that the amount of the carbon dioxide which is generated by the combustion is remarkably increased.

According to a preferred embodiment of the present invention, the method may further include collecting carbon dioxide by the carbon dioxide absorbent in the collecting reactor, discharging the collected carbon dioxide, and separating the carbon dioxide from the carbon dioxide absorbent to collect carbon dioxide, The separation and collection process can be performed through the desorber 401, which is further included in the above-described series reactor, but is not limited thereto. Since the carbon dioxide desorber may be a carbon dioxide desorber applied to a conventional carbon dioxide abatement apparatus, the present invention is not particularly limited thereto, and the energy level of heat input for separating carbon dioxide may be a specific kind of absorbent And the separation time may be different depending on the specific type of the absorbent. Therefore, the present invention is not particularly limited thereto.

The present invention will now be described more specifically with reference to the following examples. However, the following examples should not be construed as limiting the scope of the present invention, and should be construed to facilitate understanding of the present invention.

≪ Preparation Example 1 > - Preparation of carbonic anhydrase crosslinking complex 1

Polymer nanofiber was used as a support provided in the carbonic anhydrase crosslinking complex. Polystyrene (PS, MW = 950,400) and poly (styrene-co-maleic anhydride) (PSMA, MW = 224,000) were used as the polymer for making polymer nanofibers. Tetrahydrofuran (THF) and acetone were used as the organic solvent for dissolving the polymer. These materials were purchased from Sigma-Aldrich (St. Louis, MO, USA). Polymer nanofibers were prepared by electrospinning. The voltage operation condition of electrospinning was 7 kV, and the flow rate was 0.1 ml / hr using a syringe pump.

The polymer nanofibers prepared above were mixed with a carbonic anhydrase solution (10 mg / ml, 50 mM sodium phosphate buffer, pH 7.6) for the preparation of the carbonic anhydrase crosslinking complex. The carbonic anhydrase solution and the container containing the nanofibers were mixed at 200 rpm for 30 minutes. Then, to induce the covalent bond between the carbonic anhydrase and the maleic anhydride as the first functional group in the polymer nanofiber, Lt; / RTI >

Next, 0.5% v / v glutaraldehyde was added as a cross-linking agent to form a carbonic anhydrase crosslinking complex, and the solution was adjusted to have an ammonium sulfate solution concentration of 45% w / v in a solution as a precipitating agent, In order to facilitate the formation of binding complexes, they were reacted in a refrigerator at 4 ° C for 14 hours. Then, the solution containing the carbonic anhydrase cross-linking complex was stirred at 200 rpm for 30 minutes with 100 mM Tris buffer pH 7.6 and then washed with 100 mM PB. The enzyme-immobilized materials after all treatment were stored at 4 ° C to prepare a carbonic anhydrase crosslinking complex as shown in FIG.

≪ Example 1 >

For the preparation of the structure comprising the carbonic anhydrase crosslinking complex prepared in Preparation Example 1, a body part and a floating part having the structure as shown in FIG. 5 were prepared. Specifically, ABS (acrylonitrile-butadiene-styrene) polymer was used as the material of the body portion. The size of the body was 63 mm x 21 mm x 1 mm, and the grid used as the channel was formed into a square shape of 6 mm x 6 mm. At this time, the body part was prepared so that the first body and the second body having the same structure were stacked in the vertical direction to accommodate the carbonic anhydrase crosslinking complex of preparation example 1 between the laminated structures. In addition, ABS (acrylonitrile-butadiene-styrene) polymer was used as the material of the floating part, and the shape of the floating part was a rectangle having a size of 21 mm x 10 mm x 3 mm. At this time, an empty space in which air can enter into the inside of the floating part is prepared so that the body part can be positioned at the interface between the liquid and the gas upon coupling with the body part

 A carbonic anhydrase crosslinking complex of Preparation Example 1 was housed and fixed between the two laminated body portions in the form of a housing and a floating portion was bonded to both ends of the body portion to prepare a structure. Thereafter, a container having a gas supply portion having a diameter of 9 cm and a height of 22 cm and a diameter of 0.3 cm located at a height of 10 cm and a gas discharge portion having the same diameter as the gas supply portion was provided. pH 8.0) solution, and the structure was placed at the interface of the solution to prepare a carbon dioxide conversion reactor.

≪ Example 2 >

A carbon dioxide conversion reactor was prepared by carrying out the same procedure as in Example 1 except that the structure without the carbonic anhydrase cross-linking complex was placed at the interface between the solution and the gas.

<Experimental Example>

The carbon dioxide conversion reaction was induced by injecting gaseous carbon dioxide at a rate of 200 mL / min for 20 minutes through the gas supply unit of the carbon dioxide conversion reactor according to the embodiment. After 20 mL of the reaction solution was extracted, the carbonate was precipitated by reacting with 10 mL of a 670 mM calcium chloride solution. The precipitated carbonate was centrifuged at 15000 rpm for 15 minutes, and then the liquid phase was removed. The separated carbonates were dried in an oven at 90 DEG C for 24 hours and weighed to be shown in Table 1 below.

Example 1 Example 2 Weight of converted calcium carbonate (mg) 214 114

As can be seen from the above Table 1, it can be confirmed that the conversion reactor equipped with the carbonic anhydrase crosslinking complex has a carbon dioxide conversion efficiency of 1.9 times greater than that of Example 2 which does not include the carbonic anhydrase crosslinking complex.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

1: Floating structure 10: Body part
11: first body 13, 23: opening
15, 25: protrusion 21: second body
30: Floating portion 31: Part 1 Fluid
33, 37: projections 33a, 37a:
35: Part 2 Fluid 101: Conversion Reactor
111: gas supply unit 121: enzyme reaction unit
121a: Structure 121b: Liquid
131: Bicarbonate aqueous solution discharge part 141: Gas discharge part
151: reaction chamber 201: collection reactor
211: Carbon dioxide capture discharge unit 221: Gas supply unit
231: Reaction chamber 301: Bicarbonate aqueous solution reservoir
401: Desorbing machine

Claims (19)

An empty reaction chamber inside;
A gas supply unit located at one side of the reaction chamber and located at one side of the reaction chamber and directly connected to the carbon dioxide generating source to supply an exhaust gas containing carbon dioxide emitted from the carbon dioxide generating source into the reaction chamber;
A gas discharge unit positioned at the other side of the reaction chamber and discharging exhaust gas flowing into the reaction chamber; And
And a carbonic anhydrase for promoting the conversion of carbon dioxide without interfering with the liquid filled in the inner part of the reaction chamber and the flue gas flowing from the one side to the other side for the reaction of converting the carbon dioxide in the flue gas into the bicarbonate ion, And an enzyme reaction part including a structure located at an interface between the gas in the empty space of the reaction chamber and the liquid,
The gas supply unit and the gas discharge unit are located above the liquid and the structure so that the exhaust gas supplied to the gas supply unit can pass through the liquid without interfering with the flow inside the reaction chamber so as to prevent an increase in the back pressure of the conversion reactor due to the supplied exhaust gas. Wherein the structure has a flow path for allowing the liquid and the carbon dioxide to contact the carbonic anhydrase without any additional pressure,
Wherein the structure is designed to float on the liquid to be positioned at the interface with the liquid level change in the reaction chamber. The method according to claim 1,
And a bicarbonate aqueous solution discharge unit for discharging the bicarbonic acid aqueous solution converted and dissolved in the enzyme reaction unit. The method according to claim 1,
Wherein the carbonic anhydrase comprises at least one of a wild type carbonic anhydrase and a carbonic anhydrase variant. delete The method according to claim 1,
Wherein the structure further comprises a body portion including a carbonic anhydrase and at least one float coupled to the body portion so that the body portion is positioned at the interface. 6. The method of claim 5,
Wherein the body portion includes a flow path allowing liquid and carbon dioxide to contact the carbonic anhydrase. 6. The method of claim 5,
Wherein the carbonic anhydrase is bound or received on the body. The method according to claim 1,
Wherein the carbonic anhydrase is provided in any one or more of a plurality of uncrosslinked and aggregated enzyme aggregates and an enzyme crosslinking complex in which a plurality of the enzyme aggregates are mutually combined. The method according to claim 1,
The structure further includes a body portion,
Wherein the carbonic anhydrase further comprises a support and is bonded to or supported within the support,
Wherein the support is coupled or received on the body portion. 10. The method of claim 9,
Wherein the support comprises at least one selected from the group consisting of polymer fibers, electrically conductive polymers, porous particles, spherical particles, nanoparticles, beads, carbon nanotubes, wires, filaments, graphene, Conversion reactor. 9. The method of claim 8,
Wherein the enzyme cross-linking complex is formed using a precipitating agent and a cross-linking agent, further comprising a first support having a first functional group on its surface,
And a second carbonic anhydrase crosslinking enzyme which is bound to the first carbonic anhydrase and binds to the first carbonic anhydrase, the second carbonic anhydrase crosslinking enzyme being bound to the first functional group directly, and the second carbonic anhydrase cross- . 12. The composition of claim 11, wherein the enzyme cross-linking complex comprises
And a second support which comprises a second functional group on its surface and which binds to at least one of the first carbonic anhydrase and the second carbonic anhydrase crosslinking complex through the second functional group, . 3. The method of claim 2,
Further comprising at least one of a bicarbonate aqueous solution reservoir and a bicarbonate aqueous solution solution reservoir to communicate with the bicarbonate aqueous solution discharge portion. delete (1) supplying an exhaust gas to a gas supply unit of the carbon dioxide conversion reactor according to any one of claims 1 to 3 and 5 to 13; And
(2) Some of the carbon dioxide contained in the supplied exhaust gas is converted to bicarbonate ions, and the exhaust gas containing unreacted remaining carbon dioxide passes through the upper portion of the liquid without passing through the partially filled liquid in the carbon dioxide conversion reactor, Carbon dioxide conversion process. 16. The method of claim 15,
In the step (1), the flue gas is supplied from the upper portion of the liquid in the conversion reactor to prevent the increase of the back pressure of the reactor due to the flue gas supplied to the conversion reactor, and the carbon dioxide in the flue gas supplied is located at the interface between the liquid inside the conversion reactor and the gas A carbon dioxide conversion process in which a conversion reaction to bicarbonate ions is promoted through a carbonic anhydrase provided in the structure. A conversion reactor according to any one of claims 1 to 3 and 5 to 13; And
And a collection reactor communicating with the conversion reactor and collecting the introduced carbon dioxide,
The exhaust gas containing carbon dioxide is supplied to a conversion reactor or a collection reactor to convert or capture carbon dioxide, and then an exhaust gas containing unreacted carbon dioxide is introduced into a collection reactor or a conversion reactor to collect carbon dioxide which collects or converts the unreacted carbon dioxide A series reactor for conversion and collection. 18. The method of claim 17,
Wherein the collection reactor comprises at least one of a carbon dioxide absorbent and a carbon dioxide separation membrane. 18. The method of claim 17,
Wherein the collection reactor comprises a carbon dioxide collection outlet for discharging a collection containing at least one of a carbon dioxide sorbent, a carbon dioxide intercalation compound and a reactive compound, and a carbon dioxide collection outlet for communicating with the carbon dioxide collection outlet, Further comprising a carbon dioxide desorber for separating and collecting carbon dioxide.

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