WO2015099432A1

WO2015099432A1 - Multi-pipe type carbon dioxide capture device

Info

Publication number: WO2015099432A1
Application number: PCT/KR2014/012769
Authority: WO
Inventors: 조형희; 문호규; 유환주; 최원춘; 강나영; 박용기; 서휘민; 박선영
Original assignee: 연세대학교 산학협력단
Priority date: 2013-12-24
Filing date: 2014-12-23
Publication date: 2015-07-02
Also published as: KR101480654B1

Abstract

A carbon dioxide capture device of the present invention is a carbon dioxide capture device for selectively separating carbon dioxide from exhaust gas including the carbon dioxide, and comprises a plurality of carbon dioxide absorption and desorption units in which carbon dioxide absorption and carbon dioxide desorption continuously occur while a filled carbon dioxide absorbent circulates in an absorption reactor and a desorption reactor, wherein: absorption heat generated from an absorption reactor of at least one carbon dioxide absorption and desorption unit is transferred to a desorption reactor of another carbon dioxide absorption and desorption unit such that a mutual heat exchange occurs; and the absorption reactor, in which the mutual heat exchange occurs, is inserted into the desorption reactor, or the desorption reactor is inserted into the absorption reactor.

Description

Multi-tubular CO2 Collector

The present invention relates to a carbon dioxide capture device, and more particularly to a carbon dioxide capture device that can selectively collect and separate the carbon dioxide contained in the exhaust gas.

Recently, due to global warming, the sea level is rising as the polar glaciers are melting, and due to climate change, extreme weather is occurring everywhere in the world. Such global warming is known to be caused by greenhouse gas emissions such as carbon dioxide, and international conventions for regulating the amount of carbon dioxide are being signed, and the suppression of carbon dioxide emissions by introducing carbon credits has become a national economic issue. . Efforts to reduce carbon dioxide emissions are directed towards developing alternative energy sources to replace fossil fuels, such as solar and wind energy, and to capture and store carbon dioxide from fossil fuels without releasing them into the atmosphere. It is becoming. The latter technique is called carbon capture and storage (CCS) technology, which is largely divided into technology in the field of capturing carbon dioxide generated from a power plant or steel mill and storage of carbon dioxide in the ground or the ocean. Lose.

CO2 capture technology can be divided into post-combustion capture, pre-combustion capture and pure oxygen capture according to the application of the capture step, and membrane separation technology (membrane separation) that concentrates using a membrane according to the principle of capturing carbon dioxide, amine Or liquid phase separation using liquid adsorbents such as ammonia water, or solid phase separation using solid adsorbents such as alkali or alkaline earth metals.

Dry capture technology consists of the development of solid state adsorbents with carbon dioxide adsorption capacity and the process of capturing carbon dioxide using these solid state adsorbents, and the carbon dioxide collection efficiency is greatly influenced by the composition of the adsorption process as well as the performance of the solid state adsorbent. The solid phase adsorbent may be broadly classified into organic, inorganic, carbon, organic-inorganic hybrid, and the like, and may be classified into physical adsorbents and chemical adsorbents according to the type of carbon dioxide adsorbed on the adsorbent. An organic adsorbent is an amine polymer adsorbent, an inorganic adsorbent is a zeolite-based, alkali or alkaline earth metal-based adsorbent, a carbon-based adsorbent is an activated carbon-based adsorbent modified with an alkali metal, an organic-inorganic hybrid adsorbent is MOF, Porous silica adsorbents grafted with organic materials having amine groups are mainly used. Zeolite and carbon-based adsorbents exhibit the physical adsorption characteristics of carbon dioxide, and other adsorbents exhibit the chemical adsorption characteristics that carbon dioxide reacts with the adsorbent chemically. (Energy Environ. Sci. 2011, 4, 42. ChemSusChem 2009, 2, 796.)

Dry capture technology consists of adsorbing carbon dioxide to an adsorbent object and desorbing and separating the adsorbed carbon dioxide. Adsorption and desorption of carbon dioxide can occur reversibly. Adsorption and desorption of carbon dioxide can be induced through heat exchange or changes in external pressure. The process of capturing carbon dioxide using a dry adsorbent is a pressure swing adsorption (PSA) process using a pressure difference as a method for desorbing adsorbed carbon dioxide, and a temperature swing adsorption (Temperature Swing Adsorption) method using a temperature difference. TSA) process. In general, the pressure swing adsorption process using a fixed bed adsorption tower is advantageous for the capture of small scale carbon dioxide, but the fluidized bed adsorption and desorption can be easily scaled up when a large amount of carbon dioxide is emitted, such as a power plant or a large combustion furnace. A tower temperature swing adsorption process is advantageous.

The present invention aims to continuously capture a large amount of carbon dioxide using a solid adsorbent, and may be classified into a temperature swing adsorption process consisting of a fluid adsorption tower and a fluid desorption tower. Adsorption towers and desorption towers used in the temperature swing adsorption process may be classified into a bubbled fluidized bed having a high adsorbent concentration and a diluted fluidized bed having a low adsorbent concentration, depending on the operating area. When the bubble fluidized bed and the high-speed fluidized bed are applied to the adsorption tower and the desorption column, four combinations of i) a high-speed fluidized bed-high fluidized bed, ii) a high-speed fluidized bed-bubbled fluidized bed, iii) a bubbled fluidized bed-high-speed fluidized bed, and iv) a bubbled fluidized bed-bubble fluidized bed Can be derived ("Fluidization Engineering", D. Kunii and O. Levenspiel, Robert E. Krieger, 1977).

Prior arts related to this include Korean Patent Publication Nos. 2005-0003767, 2010-0099929, 2011-0054948, etc. In the prior art, a high-speed fluidized bed adsorption tower for capturing carbon dioxide using a dry dry adsorbent and Disclosed is a carbon dioxide fluidized bed collection process of a temperature swing adsorption concept composed of a bubble fluidized bed desorption tower. However, the dry capture process of the temperature swing adsorption concept requires enormous energy of 2 GJ / t-CO ₂ or more to desorb the carbon dioxide adsorbed to the adsorbent to the temperature swing adsorption process, which increases the cost of the capture together with the adsorbent cost. It acts as a factor. Therefore, in order to lower the collection cost, it is very important to develop a technology capable of effectively desorbing carbon dioxide adsorbed from the adsorbent with low energy.

Therefore, the first problem to be solved by the present invention is to use the heat generated in the adsorption process of carbon dioxide in the desorption process of carbon dioxide, carbon dioxide capture that can reduce the energy required for carbon dioxide capture and separation by making this heat exchange efficiently. To provide a device.

The second problem to be solved by the present invention is to provide a carbon dioxide capture device that can be transferred to the reactor in which desorption of carbon dioxide occurs while effectively preventing the heat generated in the reactor in which the adsorption of carbon dioxide occurs to the outside.

The third problem to be solved by the present invention is to provide a carbon dioxide capture device to improve the heat exchange efficiency by forming a vortex or turbulence in the movement of the carbon dioxide and the adsorbent packed in the reactor.

The present invention is a carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide in order to achieve the first object, the adsorption of carbon dioxide and carbon dioxide desorption while the filled carbon dioxide adsorbent circulates the adsorption reactor and desorption reactor A plurality of carbon dioxide adsorption and desorption unit continuously occurring, the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is transferred to the desorption reactor of the other carbon dioxide adsorption and desorption unit to perform mutual heat exchange, and the adsorption reactor in which the mutual heat exchange is performed Provided is a carbon dioxide capture device is inserted into the desorption reactor, the desorption reactor is inserted into the adsorption reactor.

According to one embodiment of the present invention, the adsorption reactor in which the mutual heat exchange is performed may be inserted into the center of the desorption reactor.

According to another embodiment of the present invention, the adsorption reactor in which the mutual heat exchange is made of a plurality of bundles, the adsorption reactor consisting of the plurality of bundles may be uniformly inserted into the desorption reactor.

According to another embodiment of the present invention, the desorption reactor of another carbon dioxide adsorption desorption unit is inserted into the desorption reactor inserted into the desorption reactor, or the desorption of other carbon dioxide into the desorption reactor into which the adsorption reactor is inserted A negative adsorption reactor can be inserted.

According to another embodiment of the present invention, the vortex forming means may be formed on the wall surface of the adsorption reactor or the desorption reactor in which the mutual heat exchange is performed.

According to another embodiment of the present invention, a protrusion or a depression may be formed on the wall surface of the adsorption reactor or the desorption reactor in which the mutual heat exchange is performed.

The present invention is a carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide, in order to achieve the second object, the carbon dioxide adsorption of the carbon dioxide adsorption and carbon dioxide desorption while circulating the adsorption reactor and desorption reactor A plurality of carbon dioxide adsorption and desorption unit that occurs continuously, the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is transferred to the desorption reactor of the other carbon dioxide adsorption and desorption unit to form a mutual heat exchange, the adsorption reactor and the desorption reactor is tubular It consists of, and the adsorption reactor is a mutual heat exchange is provided to surround the outer surface of the desorption reactor, or the desorption reactor provides a carbon dioxide capture device, characterized in that installed to surround the outer surface of the adsorption reactor.

According to one embodiment of the present invention, a protrusion or a depression may be formed on the outer surface or the inner surface of the adsorption reactor or the desorption reactor.

The present invention is a carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide in order to achieve the third object, the carbon dioxide adsorbent filled with the adsorption and carbon dioxide desorption while circulating the adsorption reactor and desorption reactor And a plurality of carbon dioxide adsorption and desorption units which are continuously generated, and the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is transferred to the desorption reactor of the other carbon dioxide adsorption and desorption unit, whereby mutual heat exchange is performed. Provided is a carbon dioxide capture device characterized in that a protrusion or a depression for forming a vortex in the desorption reactor is formed.

The carbon dioxide capture device of the present invention has the following effects.

1. The carbon dioxide capture device of the present invention uses heat generated in the adsorption process of carbon dioxide in the desorption process of carbon dioxide, thereby reducing energy consumption.

2. The heat exchange can be efficiently performed because the adsorption reactor in which heat exchange is performed during the adsorption and desorption of carbon dioxide is inserted into the desorption reactor or the desorption reactor is inserted into the adsorption reactor.

3. Adsorption reactor that exchanges heat during the adsorption and desorption of carbon dioxide covers the outer surface of the desorption reactor, or desorption reactor covers the outer surface of the adsorption reactor, thereby reducing the heat leakage to the outside.

4. In the adsorption and desorption process of carbon dioxide, the adsorption reactor which performs heat exchange is inserted into the desorption reactor consisting of a plurality of tubular shapes, or the desorption reactor is composed of a plurality of tubular shapes and inserted into the adsorption reactor. It is possible to improve the heat exchange efficiency.

5. Desorption reactors are installed at the same time both inside and outside of the adsorption reactor where carbon dioxide adsorption takes place, allowing for more efficient heat exchange.

1 is a view for explaining the concept that the heat exchange between the adsorption reactor and the desorption reactor in the carbon dioxide capture device of the present invention.

Figure 2 shows a carbon dioxide capture device in which the adsorption reactor is inserted into the desorption reactor.

3 illustrates a carbon dioxide capture device in which a plurality of adsorption reactors are inserted into a desorption reactor.

4 illustrates a carbon dioxide capture device in which a desorption reactor is installed inside and outside the adsorption reactor.

5 illustrates a carbon dioxide capture device in which a desorption reactor is installed outside and inside the adsorption reactor, and the adsorption reactor is installed outside the desorption reactor.

FIG. 6 is a view for explaining heat exchange occurring in a structure in which a lip turbulator is installed on a wall of an adsorption reactor or a desorption reactor.

Figure 7 shows various configurations of the lip turbulator that can be applied to the carbon dioxide capture device of the present invention.

8 shows a continuous ring type lip turbulator and an inner continuous groove type turbulator.

FIG. 9 is a view for explaining changes in gas flow and solid flow generated by the lip turbulator.

10 is a view showing radial particle distribution in a high speed fluidized bed reactor in operation.

FIG. 11 is a view for explaining a process in which heat exchange occurs on a wall of a reactor in which a protrusion and a depression type turbulator are installed.

It is a figure for demonstrating the arrangement | positioning method of a protrusion and a recessed part.

FIG. 13 is a view for explaining changes in gas flow and solid flow that occur in a turbulator having a gentle inclination angle at the start of the protrusion.

FIG. 14 is a view for explaining changes in gas flow and solid flow that occur in a turbulator having a gentle inclination angle at the start of the depression.

15 is a view for explaining the height and arrangement interval of the lip in the reactor to which the lip turbulator is applied.

FIG. 16 is a view for explaining the height of the protrusion, the depth of the recess, and the arrangement interval in the reactor to which the protrusion and the recess are applied.

The carbon dioxide capture device of the present invention is a carbon dioxide capture device for selectively separating carbon dioxide from a flue gas containing carbon dioxide, and a plurality of carbon dioxide adsorption and carbon dioxide desorption occur continuously while a packed carbon dioxide adsorbent circulates through an adsorption reactor and a desorption reactor. A carbon dioxide adsorption desorption unit, and the heat of adsorption generated in the adsorption reactor of at least one carbon dioxide adsorption desorption unit is transferred to another desorption reactor of the other carbon dioxide adsorption / desorption unit to perform mutual heat exchange, and the adsorption reactor in which the mutual heat exchange is performed is inserted into the desorption reactor. Or, the desorption reactor is inserted into the adsorption reactor.

The present invention is to maintain and improve the heat exchange efficiency (when the process is large) of the gas-adsorbent heat exchange type fluidized bed reactor (bubble fluidized bed or high-speed fluidized bed) for the multi-stage carbon dioxide dry capture process configuration. The present invention carbon dioxide through heat exchange in a multi-stage carbon dioxide dry capture process As a method for increasing the use of the reaction heat generated during the adsorption reaction, the heat exchange efficiency for the process configuration may be maintained as the size of the multi-stage carbon dioxide dry capture process reactor increases. More specifically, the present invention provides a method for constructing a multi-tubular heat exchange type fluidized bed reactor for a multi-stage carbon dioxide dry capture process and a method for improving heat transfer at the reactor wall, and a desorption reaction with a carbonation reactor in which an exothermic reaction occurs and an endothermic reaction occurs. In order to maximize the contact area with the adsorbent inside the reactor, the adsorption reactor can be configured in multiple (multi-tube-bundled) forms. Alternatively, the carbon dioxide adsorption reactor in which the exothermic reaction takes place may be manufactured in an annular form and a desorption reactor may be installed on the inner and outer surfaces of the reactor. Furthermore, a rib turbulator as a vortex forming means that is a heat transfer improving device on the wall of the heat exchanger for improving heat transfer on the wall of such a heat exchange type fluidized bed reactor (double pipe, multi pipe (bundle), annular (triple pipe, quadruple)). ), Groove type turbulators, protrusions, and depressions can be formed in multiple arrangements.

Hereinafter, the present invention will be described in more detail with reference to the drawings.

1 is a view for explaining the concept that the heat exchange between the adsorption reactor and the desorption reactor in the carbon dioxide capture device of the present invention. Referring to Figure 1, the carbon dioxide capture device is composed of three stages of low temperature, medium temperature, high temperature stage. In each stage, the adsorbent is circulated between the reactor where the adsorption of carbon dioxide occurs and the reactor where desorption of carbon dioxide occurs, and the heat of reaction generated during the adsorption reaction at the high temperature of the upper stage is used as energy for the desorption reaction of carbon dioxide. . Although not shown in the figure, the outside of the desorption reactor may be provided with a heat insulating means for preventing the external leakage of heat.

Figure 2 shows a carbon dioxide capture device in which the adsorption reactor is inserted into the desorption reactor. Referring to FIG. 2, the carbon dioxide adsorption reactor is configured to be inserted into the carbon dioxide desorption reactor, where the heat of adsorption is generated while the adsorbent of the adsorption reactor adsorbs carbon dioxide, and the heat is desorbed through the wall of the adsorption reactor. Desorption of carbon dioxide from the adsorbent is carried to the reactor. In this case, the adsorption reactor and the desorption reactor shown in the drawings are adsorbing reactors and desorption reactors of different temperature stages adjacent to each other, and the adsorbents packed in the adsorption reactor and the adsorbents packed in the desorption reactor are different from each other. Have. To this end, the adsorbents having different temperature adsorption and desorption temperatures may be made of different materials, different crystalline materials, different doping materials may be used, or different doping amounts. The structure of the adsorption reactor and the desorption reactor in which the mutual heat exchange is performed is preferably such that the adsorption reactor is inserted into the center of the desorption reactor in view of the efficiency of heat exchange. In the drawings, the adsorption reactor is inserted into the desorption reactor in the form of the reactor, the desorption reactor may be modified to be inserted into the adsorption reactor, the desorption reactor wraps the outer surface of the adsorption reactor, or the adsorption reactor is desorption reactor If the shape surrounding the outer surface of the reactor can be modified in various forms.

3 illustrates a carbon dioxide capture device in which a plurality of adsorption reactors are inserted into a desorption reactor. Referring to Figure 3, the adsorption reactor is composed of a plurality of tubular reactor, it is installed in the form inserted into the desorption reactor. In this case, the heat generated in the adsorption reactor is transferred to the desorption reactor as described in FIG. 2, but the external area of the adsorption reactor may be increased to improve heat exchange efficiency. The number of adsorption reactors can be varied, and the arrangement of adsorption reactors can also be varied in consideration of heat exchange efficiency. In addition, the diameter of the adsorption reactor may be designed differently in consideration of heat exchange efficiency. This type of reactor is advantageous for the large size of the reactor. This is because the larger the diameter of the reactor, the larger the area where heat exchange takes place. The plurality of adsorption reactors inserted into the desorption reactor are preferably inserted in the inside of the desorption reactor in consideration of heat exchange efficiency.

4 illustrates a carbon dioxide capture device in which a desorption reactor is installed inside and outside the adsorption reactor. Referring to FIG. 4, the adsorption reactor is formed in an annular shape, a larger diameter annular desorption reactor is installed outside the adsorption reactor, and a tubular desorption reactor is installed in the inner space of the adsorption reactor. In this embodiment, the heat generated in the adsorption reactor is similar to that of FIGS. 3 and 4, but heat exchange is performed inside and outside the adsorption reactor, thereby improving heat exchange efficiency. Although not shown in the drawings, the embodiment of the present invention shown in FIG. 3 and the embodiment shown in FIG. 4 are combined, that is, a plurality of cyclic adsorption reactors having a desorption reactor installed therein, and these adsorption reactors are desorption. It is also possible to construct a carbon dioxide capture device installed in the form inserted in the reactor.

5 illustrates a carbon dioxide capture device in which a desorption reactor is installed outside and inside the adsorption reactor, and the adsorption reactor is installed outside the desorption reactor. Referring to FIG. 5, the adsorption reactor and the desorption reactor are sequentially inserted, and heat is transferred from the adsorption reactor to the desorption reactor. Although not shown in the drawings, the number of adjacent installations of the adsorption reactor and the desorption reactor may be increased, which may be more necessary when the reactor is enlarged. In addition, a multiple adsorption reactor of the type shown in FIG. 3 may be applied to the reactor having such a structure.

FIG. 6 is a view for explaining heat exchange occurring in a structure in which a lip turbulator is installed on a wall of an adsorption reactor or a desorption reactor. 6A is a reactor having a structure in which no lip turbulator is formed, and (B) is a reactor having a structure in which a lip turbulator is formed. Referring to Figure 6 (a), the temperature of the adsorption reactor is driven higher than the temperature of the desorption reactor, the heat flow is generated by the temperature difference formed along the wall surface of the adsorption reactor or the wall of the desorption reactor. Referring to FIG. 6B, a lip turbulator is installed on the wall surface of the adsorption reactor or the wall surface of the desorption reactor. The lip turbulator is formed to protrude from the wall, and forms a vortex in the gas flow and the adsorbent flow inside the reactor to effectively transfer heat from the adsorbent or gas to the wall of the reactor, and the heat transfer wall. By increasing the surface area of the function to improve the heat exchange efficiency.

Figure 7 shows the configuration of the lip turbulator that can be applied to the carbon dioxide capture device of the present invention. Referring to FIG. 7, (a) of FIG. 7 illustrates a structure in which lip turbulators are continuously formed side by side in a longitudinal direction on the outer surface or the inner surface of the reactor (inlined array, continuous rib), and (b) The turbulator is formed in the form of broken side by side (inlined array, discreted rib), (C) is the structure in which the lip turbulator is staggered (Staggered array), and (D) is the lip turbulator with the slope (Angled array, continuous rib), (e) is the structure where the lip turbulator is bent and broken with an inclination (Angled array, discrete rib), and (bar) is the lip turbulator is inclined. (Angled array, discreted rib), and (g) is a structure in which the lip turbulator is continuously formed in the shape of being bent from the top with an inclination (Angled array, conti) nuous rib), (a) is a structure in which the lip turbulator is inclined upwardly with a slope and is continuously formed (Angled array, continuous rib). (Angled array, continuous rib), (car) is a continuous structure in which the lip turbulator is inclined (Diagonal array, continuous rib), (ka) is in the form that the lip turbulator has a slope (Diagonal array, continuous rib), (ta) is a structure in which the lip turbulator is formed in a continuous vertical form (Vertical array, continuous rib), (below) is a structure in which the lip turbulator is formed in a broken vertical form (Vertical array, discrete rib). Each embodiment may be selected or combined in consideration of the density, size, temperature, etc. of the adsorbent. Referring to FIG. 7 (G), the sectional structure of the lip turbulator can also be configured in various ways. The sectional shape of the lip turbulator may be formed in a quadrangular, trapezoid, triangle, or circular shape, or the shape of the lip turbulator may be roundly deformed in the figure. Can be done.

8 shows a turbulator of a continuous ring type lip and an inner continuous groove type turbulator. 8A shows a continuous ring type rib turbulator formed on the outside of the carbon dioxide adsorption reactor, and (b) shows a continuous groove type turbulator inside the carbon dioxide adsorption reactor. (continuous groove) is formed. The continuous ring-type lip turbulator or the continuous groove-type turbulator may be in the form of a plurality of rings formed in parallel or helically connected. The outer continuous ring type lip turbulator can change the adsorbent flow inside the carbon dioxide desorption reactor, and the inner continuous groove type turbulator can change the adsorbent flow inside the adsorption reactor. Such continuous lip turbulators and groove type turbulators have a residence time of particles (cluster form) near the wall in a high-flow fluidized bed reactor in which core-annular particle distributions occur. The contact rate can be increased to improve bed-to-wall or wall-to-bed heat transfer characteristics.

FIG. 9 is a view for explaining changes in gas flow and solid flow generated by the lip turbulator. FIG. 9A is a diagram of a reactor of a high density bed (bubble fluidized bed) type, and (B) is a diagram of a reactor of a low density bed (rapid fluidized bed) type. Referring to (a) of FIG. 9, the adsorbent is filled into the reactor at a high density, and the solid flow, which is the flow of the adsorbent, is formed from the top to the bottom, and the adsorbent moves while contacting the lip turbulator. Therefore, the time required for heat exchange is increased and the contact area required for heat exchange is also increased, resulting in improved heat exchange efficiency. In addition, a gas flow that is formed in the opposite direction to the solid flow also forms a vortex near the lip turbulator. Referring to (b) of FIG. 9, the adsorbent is filled with a low density inside the reactor so that there is an empty space between the adsorbents and moves inside the reactor (movable in the form of a cluster), but also in contact with the lip turbulator In addition, heat exchange can occur more efficiently as the probability of separation of cluster-type absorbents by vortex formation increases.

10 is a diagram showing radial particle distribution in a high speed fluidized bed reactor in operation (Wirth and Seiter, 1991). A thin air layer (approximately particle free zone) of about 0.2-0.9 mm is present on the wall of the reactor, which acts as a resistance to heat transfer by particles (cluster or strand-annuls region). Therefore, by installing the structure on the wall of the reactor, vortex generation is induced to break the thin air layer on the wall or to install a protrusion-type structure in the wall region with falling strands to increase the probability of contact with the reactor. It is possible to increase heat transfer by increasing the residence time of the particles or by increasing the residence time of the particles.

FIG. 11 is a view for explaining a process of heat exchange occurring in a lip turbulator of a protrusion and a depression type. FIG. 11A is a case where a depression is formed on the wall boundary between the adsorption reaction portion and the desorption reaction portion, and (B) is a case where a protrusion is formed on the wall boundary between the adsorption reaction portion and the desorption reaction portion. The contact area with the adsorbent is increased by the protrusions or depressions, and the heat transfer efficiency may be increased by the vortex formation. Although not shown in the drawings, protrusions and depressions may be formed together on the surface of the adsorption reactor or desorption reactor, protrusions may be formed on the adsorption reactor, and depressions may be formed on the desorption reactor, and vice versa.

It is a figure for demonstrating the arrangement | positioning method of a protrusion and a recessed part. Referring to FIG. 12, the arrangement of the protrusions and the depressions formed in the reactor may be formed by forming the protrusions and the depressions on the same horizontal line and alternating in the longitudinal direction as shown in (A), and the horizontal lines as shown in (B). It is also possible to form alternately in the longitudinal direction. In addition, in consideration of the temperature difference formed in the reactor in the longitudinal direction, it is also possible to change the formation density, the formation size, and the like of the protrusion and the depression.

It is a figure for demonstrating the change of the gas flow and solid flow which are made in the protrusion protrusion of a gentle shape of the starting part inclination angle of a protrusion. 13A is a phenomenon occurring in a high density bed (bubble fluidized bed), and (B) is a phenomenon occurring in a low density bed (high speed fluidized bed). Vortex occurs in the gas flow and the solid flow along the slope of the protrusion. In the high velocity fluidized bed, groups of particles in the form of clusters or strands may flow down near the protrusions to separate the group of particles by vortices by the protrusions, thereby increasing heat transfer between the single particles and the wall surface. Since the inclination angle of the starting portion of the protrusion is formed smoothly, the collision angle with the protrusion is small, and thus the adsorbent can be prevented from being broken by the collision.

14 is a view for explaining the change in the gas flow and the solid flow made in the depression turbulence (gradle) of the gentle start portion inclination angle. 14A is a phenomenon occurring in a high density bed (bubble fluidized bed), and (B) is a phenomenon occurring in a low density bed (high speed fluidized bed). Vortex occurs in the gas flow and the solid flow along the slope of the depression. In addition, an increase in the contact area can be expected to increase heat transfer. Since the inclination angle of the start portion of the depression is formed gently, it is possible to prevent the adsorbent from being broken by the collision.

15 is a view for explaining the height and arrangement interval of the lip in the reactor to which the lip turbulator is applied. The height (e) of the lip is preferably at least the thickness of the air layer (0.2 to 0.9 mm) between the reactor wall and the adsorbent group (annulus) generated during the high-speed fluidized bed operation, and the height above the predetermined height is reduced to reduce the attrition of the absorbent. It is preferable not to exceed it. Considering these factors, it is desirable that the appropriate lip height be about 1 to 10 times the diameter of the adsorbent (Geldart group A particles: average adsorbent diameter of 100 to 200 micrometers). The preferred arrangement spacing P of the ribs is preferably 2 ≦ P / e ≦ 100. The spacing is the spacing necessary for the infiltration of particles or reattachment of flow between the lip, and the infiltration of particles and reattachment of flow can improve heat transfer. The shape of the lip to be installed is preferably made of a smooth (round) to reduce the consumption of the adsorbent, it may be made of a soft material to reduce the consumption or destruction of the adsorbent.

FIG. 16 is a view for explaining the height of the protrusion, the depth of the recess, and the arrangement interval in the reactor to which the protrusion and the recess are applied. The height e of the protrusion is preferably at least the thickness of the air layer (0.2 to 0.9 mm) between the reactor wall and the adsorbent group (annulus) generated during the high-speed fluidized bed operation, and the height above the predetermined height is reduced in order to reduce the attrition of the absorbent. It is preferable not to exceed it. Considering these factors, it is preferable that the height of the appropriate protrusion is about 1 to 10 times the diameter of the adsorbent (Geldart group A particles: average adsorbent diameter of 100 to 200 micrometers). The depth of the depression can be designed to be equal to the height of the protrusion. Preferably, the arrangement interval P of the protrusions and recesses is 2 ≦ P / e ≦ 100. The spacing is the spacing necessary for the infiltration of particles or reattachment of flow between the lip, and the infiltration of particles and reattachment of flow can improve heat transfer. The protrusions and recesses to be installed are preferably made of a smooth curved round to reduce the consumption of the adsorbent, and may be made of a soft material to reduce the consumption or destruction of the adsorbent.

The above description has been made using the embodiments of the technical idea of the present invention, and those skilled in the art to which the present invention pertains various modifications and variations without departing from the essential characteristics of the present invention. Therefore, the embodiments described in the present invention are not intended to limit the technical spirit of the present invention but to describe the present invention, and the scope of the technical idea of the present invention is not limited by these embodiments. The protection scope of the present invention should be interpreted by the claims, and all technical ideas within the equivalent scope should be interpreted as being included in the scope of the present invention.

Claims

In the carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide,

The packed carbon dioxide adsorbent includes a plurality of carbon dioxide adsorption and desorption units in which carbon dioxide adsorption and carbon dioxide desorption occur continuously while circulating the adsorption reactor and the desorption reactor, and the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is different. It is transferred to the negative desorption reactor to exchange heat with each other,

The adsorption reactor in which the mutual heat exchange is performed is inserted into the desorption reactor, or the desorption reactor is inserted into the adsorption reactor.
The method according to claim 1,

The adsorption reactor in which the mutual heat exchange is performed is inserted into the center of the desorption reactor.
The method according to claim 1,

The adsorption reactor in which the mutual heat exchange is made of a plurality of bundles, carbon dioxide trapping device characterized in that the adsorption reactor consisting of a plurality of bundles is uniformly inserted into the desorption reactor.
The method according to claim 1,

The desorption reactor of another carbon dioxide adsorption desorption unit is inserted into the adsorption reactor inserted into the desorption reactor,

Carbon dioxide capture device, characterized in that the adsorption reactor of the other carbon dioxide adsorption and desorption part is inserted into the desorption reactor in which the adsorption reactor is inserted.
The method according to claim 1,

And a vortex forming means is formed on the wall surface of the adsorption reactor or the desorption reactor in which the mutual heat exchange is performed.
The method according to claim 1,

The carbon dioxide collecting device, characterized in that the protrusion or the depression is formed on the wall surface of the adsorption reactor or the desorption reactor is a mutual heat exchange.
In the carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide,

The packed carbon dioxide adsorbent includes a plurality of carbon dioxide adsorption and desorption units in which carbon dioxide adsorption and carbon dioxide desorption occur continuously while circulating the adsorption reactor and the desorption reactor, and the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is different. It is transferred to the negative desorption reactor to exchange heat with each other,

And the adsorption reactor and the desorption reactor are tubular, and the adsorption reactor in which the mutual heat exchange is performed surrounds the outer surface of the desorption reactor, or the desorption reactor is installed to surround the outer surface of the adsorption reactor.
The method according to claim 7,

Carbon dioxide capture device characterized in that the protrusion or depression formed on the outer surface or the inner surface of the adsorption reactor or desorption reactor.
In the carbon dioxide capture device for selectively separating the carbon dioxide from the exhaust gas containing carbon dioxide,

The packed carbon dioxide adsorbent includes a plurality of carbon dioxide adsorption and desorption units in which carbon dioxide adsorption and carbon dioxide desorption occur continuously while circulating the adsorption reactor and the desorption reactor, and the heat of adsorption generated in the adsorption reactor of the at least one carbon dioxide adsorption and desorption unit is different. It is transferred to the negative desorption reactor to exchange heat with each other,

And a protrusion or a depression for forming a vortex in the adsorption reactor and the desorption reactor in which the mutual heat exchange is performed.