KR101808166B1 - Apparatus for fixing catalyst and circulating sorbent separately - Google Patents

Abstract

The present invention relates to an apparatus which fixes a catalyst into a reactor, and separates, regenerates, and circulates an absorbent only. The purpose of the present invention is to prevent activity deterioration, abrasion or contamination of the catalyst by fixing the catalyst into a core of a core-annular reactor and circulating the absorbent. The apparatus of the present invention comprises: the core which contains the catalyst and absorbent, into which a reaction gas is supplied, and a top portion of which is opened; a chamber which accommodates the core; and an annular which encircles the core as a space located between the core and the chamber. The supplied reaction gas generates a forming gas and steam within the core while flowing the contained catalyst and absorbent; the generated steam is absorbed by the flowing absorbent; the steam-absorbed absorbent leaves the core through the opened top portion of the core such that the steam-absorbed absorbent is contained in the annular; and the catalyst is fixed to the inside of the core.

Description

[0001] Apparatus for fixing catalyst and circulating sorbent [

The present invention relates to an apparatus comprising a reactor for reacting a reactant gas with a catalyst in an absorber atmosphere, and more particularly to an apparatus for securing a catalyst in a reactor and separating, regenerating, and circulating the absorbent only.

In general, the processes using two fluidized bed reactors include water vapor absorption and regeneration processes, carbon dioxide absorption and regeneration processes, carbon dioxide conversion processes, oxidation-reduction processes of chemical-looping combustors, absorption-promoting natural gas steam reforming Sorption enhanced steam methane reforming of natural gas process, sorption enhanced water gas shift process, and chemical-looping hydrogen generation process.

FIG. 1 is an illustration showing an apparatus for the water vapor absorption and regeneration process. Referring to FIG. 1, the apparatus comprises a reactor 100 and a regeneration reactor 200. The catalyst (93) and the absorbent (94) are accommodated in the reactor (100). The reaction gas (91) flows into the reactor (100). The introduced reaction gas flows and reacts in the reactor (100) with the catalyst (93) and the absorbent (94). That is, in the reactor 100, a catalyst-absorbent fluidized bed is formed. The introduced reaction gas reacts to generate a product gas and water vapor. The generated product gas 92 is discharged from the reactor 100, and the generated water vapor is absorbed by the flowing absorbent 94.

The absorbent 94, which has absorbed the water vapor, moves to the regeneration reactor 200 for regeneration. However, it is not easy to separate only the absorbent 94 that absorbs the water vapor from the catalyst 93 that flows together. Therefore, according to the prior art shown in FIG. 1, the catalyst 93 and the absorbent 94 absorbing the steam move together to the regeneration reactor 200. The fluidized gas 95 flows into the regeneration reactor 200 and flows the flowing catalyst 93 and the absorbent 94 in the regeneration reactor 200. And, in the regeneration reactor 200, the water vapor and the absorbent 94 are separated and become the regenerated water and the regenerated absorbent 94, respectively. Thereby, the regenerated water and the fluidizing gas (96) are discharged from the regeneration reactor (200). Then, the regenerated absorbent 94 and the catalyst 93 return to the reactor 100.

Thus, according to the prior art, since the catalyst and the absorbent circulate together, the catalyst is exposed to the environment for regenerating the absorbent (regeneration reactor). Accordingly, the catalyst may lose its activity. In addition, the catalyst may be subjected to a physical impact during its circulation to wear. In addition, the catalyst may be contaminated by various factors during the circulation. Therefore, various methods for fixing the catalyst in the reactor have been studied.

US Patent No. 9314760 (registered on April 19, 2016)

In order to solve the above problems, an object of the present invention is to fix a catalyst in a core of a core-annular reactor and to circulate the absorbent to prevent catalyst deactivation, wear and contamination.

However, the problems to be solved by the present invention are not limited to the above-described problems, and other problems that are not described can be clearly understood by those skilled in the art from the following description.

In order to achieve the above object, the present invention is constructed as follows.

A core which receives the catalyst and the absorbent, receives the reaction gas into the inside thereof and has an open top; A chamber for receiving the core; And an annulus surrounding the core, the annulus surrounding the core, wherein the supplied reactant gas creates a product gas and water vapor while flowing the accommodated catalyst and the absorbent, ; The generated water vapor is absorbed by the flowing absorbent; Said absorbent absorbing said water vapor escapes said core through said open top and is received in said annular; Wherein the catalyst is fixed within the core.

The generated product gas may be discharged from the chamber by leaving the core through the open top.

The absorbent contained in the annular may be withdrawn from the chamber, regenerated and then reintroduced into the chamber.

The catalyst fixing and absorbent separation and recycling apparatus may further include a gas supply unit for supplying the reaction gas into the core.

The gas supply unit may control the supply rate of the reaction gas such that the catalyst is fixed in the core and only the absorbent absorbing the vapor deviates from the core.

The catalyst fixing and absorbent separation and circulation apparatus may further comprise a regeneration reactor for regenerating the absorbent discharged from the chamber after absorbing the steam and re-introducing the regenerated absorbent into the chamber.

The regenerating reactor may include a transfer reactor for absorbing the water vapor, the absorbent discharged from the chamber, and a fluidizing gas, and discharging the introduced absorbent and the fluidizing gas.

The fluidizing gas may be inert gas or air.

The fluidized gas may transfer the introduced absorbent in the transfer reactor.

The regenerating reactor further includes a gas-solid separator for introducing the absorbent and the fluidizing gas discharged from the transferring reactor, discharging regenerated water and fluidizing gas, and recycling the regenerated absorbent into the chamber .

The gas-solid separator may be a cyclone separator or a collision separator.

The regeneration reactor may further include a condenser connected to the gas-solid separator, for discharging the condensed water by condensing the discharged regenerated water, and for passing the discharged fluidized gas.

The open top of the core may be inverted conical.

The reaction gas may include methanol and carbon dioxide.

The catalyst may comprise a copper-based catalyst or an iron-based catalyst.

The catalyst fixed in the core may be denser than the absorbent.

The catalyst fixed in the core may be larger in size than the absorbent.

The absorbent may comprise a metal oxide.

The catalyst fixing and sorbent separating and circulating device may further include a catalyst dispersing plate located in the annulus, surrounding the core bottom, and containing the catalyst.

Unreacted gas in the discharged product gas may be reintroduced into the annulus.

The catalyst fixing and absorbent separation and recycling apparatus may further include an unreacted gas separator for separating the unreacted gas from the discharged product gas so that the unreacted gas is reintroduced.

The re-introduced unreacted gas may pass through the catalyst dispersion plate so as to be dispersed while being reacted.

The absorbent that leaves the core may be seated on the catalyst dispersion plate located in the annulus.

The catalyst dispersion plate may be of a porous type, a mesh type, or a nozzle type.

The carbon dioxide absorbent may be circulated in the catalyst fixing and absorbent separation circulation apparatus.

According to one embodiment of the present invention having such a configuration, a catalyst having a large density and / or a large size is fixed in the core of the core-annular reactor, and the absorbent having a small density and / or a small size is circulated, , Abrasion, contamination, and the like can be prevented.

Also, according to one embodiment of the present invention, since the upper portion of the core is expanded more than the lower portion, the flow rate of the catalyst and the absorbent is lower at the upper portion of the core than at the lower portion. Thus, only the absorbent detaches from the core and the effect of fixing the catalyst in the core becomes greater.

Further, according to one embodiment of the present invention, there is no need for a separate device for separating the absorbent from the catalyst, and reaction of the reaction gas, absorption of water vapor (or carbon dioxide) of the absorbent, and desorption of the absorbent can be performed at the same time.

Further, according to one embodiment of the present invention, the reaction efficiency is high because the catalyst-absorbent fluidized bed is formed intensively in the core and the reaction of the reaction gas is concentrated in the core.

Also, according to an embodiment of the present invention, the unreacted gas is re-introduced and reacted through the catalyst dispersion plate, so that the reaction gas is not wasted and the process efficiency is high.

In addition, according to an embodiment of the present invention, since the reaction gas is reacted not only in the core but also in the annulus, the entire space in the core-annular reactor is efficiently utilized.

According to an embodiment of the present invention, since the absorbent desorbing the core is placed on the catalyst dispersion plate and the unreacted gas passes through the catalyst dispersion plate on which the absorbent is placed, Carbon dioxide) is absorbed. Thus, there is no need to add an absorbent for absorbing water vapor generated in the annular tube to the core-annular reactor, which results in high process efficiency.

Further, according to an embodiment of the present invention, the first circulation pump discharges the adsorbent on the catalyst dispersion plate at the second terminal speed from the chamber, so that catalyst fixation and sorbent separation is achieved not only in the core but also in the annulus. Therefore, the apparatus including the catalyst dispersion plate can prevent the catalyst deactivation, wear and contamination at the same level as that of the apparatus not including the catalyst dispersion plate, while being higher in process efficiency than the apparatus not including the catalyst dispersion plate .

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is an illustration showing an apparatus for a conventional water vapor absorption and regeneration process. FIG.
2 is a schematic view showing a circulation apparatus for separating catalyst fixing and absorbent according to an embodiment of the present invention.
FIG. 3 is a schematic view showing a state where a catalyst is fixed in a core and an absorbent is separated from the core according to an embodiment of the present invention.
4 is a schematic view showing a circulation apparatus for separating catalyst fixing and absorbent according to an embodiment of the present invention.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

For clarity of explanation of the embodiments of the present invention, parts that are not related to the description in the accompanying drawings are omitted. Like parts throughout the specification are labeled with like reference numerals.

The terminology used herein is for the purpose of describing various embodiments and is not intended to be limiting of the present invention. When the first component is said to be "connected (connected, contacted)" to a second component, this means that the first component is "directly connected" to the second component, Quot; indirectly "through < / RTI > The singular forms "a," "an," and "the" include plural referents unless the context clearly dictates otherwise. It is also to be understood that the terms " comprises "or" having ", when used in this specification, mean that there are features, numbers, steps, But does not exclude the presence or addition of one or more other features, integers, steps, operations, elements, parts, or combinations thereof.

Hereinafter, Embodiment 1 relates to a water vapor absorbent separation and circulation apparatus, and Embodiment 2 relates to an apparatus in Embodiment 1 in which a catalyst dispersion plate, an unreacted gas separator, and the like are added. The third embodiment relates to a circulation apparatus for separating carbon dioxide absorbent, and the fourth embodiment relates to an apparatus in which a catalyst dispersion plate, an unreacted gas separator, and the like are added to the apparatus of the third embodiment. The present invention can be applied not only to water vapor or carbon dioxide, but also to absorbents that absorb other gases.

[Example 1]

2 is a schematic view showing a circulation apparatus for separating catalyst fixing and absorbent according to an embodiment of the present invention. Referring to FIG. 2, the apparatus for separating catalyst fixing and absorbent according to an embodiment of the present invention includes a gas supply unit 20, a core-annular reactor 30, a regeneration reactor, and the like. The core-annular reactor 30 includes a core 31, an annular 32, and a chamber 33. The regeneration reactor comprises a transfer reactor (40), a gas-solid separator (50), and a condenser (69). First, referring to Fig. 2, the overall structure of the catalyst fixing and absorbent separation unit will be briefly described.

The gas supply 20, the transfer reactor 40, the gas-solid separator 50 and the condenser 69 are both located outside the chamber 33, 33).

One side of the gas supply part 20 is connected to one side of the lower part of the core 31 via a gas inlet part 61. The gas inlet (61) penetrates the lower side of the chamber (33).

A gas discharge portion 62 is positioned at one side of the upper portion of the chamber 33. A first connection part (63) is located on the other side of the lower part of the chamber (33). The first connection portion 63 connects the other side of the lower portion of the chamber 33 with the lower side of the transfer reactor 40. A first circulation pump (64) is located at the center of the first connection part (63).

The gas inlet 65 is located on the other side of the lower portion of the transfer reactor 40. A second connection part (66) is located above the transfer reactor (40). The second connection unit 66 connects the upper portion of the transfer reactor 40 and the upper end of the gas-solid separator 50. And a second circulation pump 67 is located at the center of the second connection portion 66.

A gas discharge port 68 is located at one side of the upper portion of the gas-solid separator 50. A solid discharge portion 71 is positioned below the gas-solid separator 50. The solid discharge portion 71 connects the lower portion of the gas-solid separator 50 and the upper portion of the chamber 33.

The other side of the condenser 69 is connected to the upper side of the gas-solid separator 50 through the gas discharger 68. A discharge unit 70 is located at one side of the condenser 69. However, the overall structure of the catalyst fixing and absorbent separation circulation apparatus can be appropriately changed by the designer. Hereinafter, referring to Fig. 2, the catalyst fixing and absorbent separation circulation apparatus will be described in more detail.

The core 31 receives the catalyst 81 and the absorbent 82. The catalyst 81 and the absorbent 82 are always solid in the process environment and may be spherical or pellet-shaped. The catalyst 81 has a higher density and / or size than the absorbent 82. The size means the diameter when the absorbent 82 is spherical, and the diameter of the section when it is pellet.

A reaction gas is supplied into the core (31). Reaction gas 2 supplied to the lower portion of the core 31 rises in the core 31 to flow the catalyst 81 and the absorbent 82. That is, in the core 31, the catalyst-absorbent fluidized bed is formed by the supplied reaction gas 2. The supplied reaction gas 2 is introduced into the core 31 while the absorbent 4 having a relatively small density and / or a small size is removed from the core 31 and the catalyst 81 having relatively high density and / (Hereinafter, referred to as " first terminal velocity "). In other words, the supplied reaction gas 2 forms the catalyst-absorber fluidized bed while the catalyst 81 is fixed in the core 31 and only the absorbent 4 is released from the core 31. In any subsequent process, the catalyst 81 having a relatively high density and / or a large size is always fixed in the core 31. Therefore, degradation of catalyst activity, abrasion, contamination, and the like can be prevented as compared with the prior art.

3 is a schematic view showing that the catalyst 81 is fixed within the core 31 and the absorbent 4 is separated from the core 31 according to an embodiment of the present invention. 3 (a), before the reaction gas is supplied into the core 31, the catalyst 81 and the absorbent 82 are stacked under the core 31 in a mixed state. Thereafter, when the reaction gas is supplied into the core 31, the catalyst 81 and the absorbent 82 flow by the reaction gas (Fig. 3 (b)). At this time, the absorbent 82 is located above the catalyst 81 in the catalyst-absorbent fluidized bed because the density and / or size of the absorbent 82 is less than the density and / or size of the catalyst 81 b)). The absorbing agent 82 is continuously pushed up by the rising reaction gas. As a result, the absorbent 4 leaves the core 31, and the catalyst 81 is fixed in the core 31 while flowing (Fig. 3 (c)).

Referring again to FIG. 2, the supplied reaction gas 2 rises in the core 31 to form a catalyst-absorbent fluidized bed, and reacts to generate a product gas and steam. The absorbent 82 flowing by the supplied reaction gas 2 absorbs the generated water vapor. The absorbent 4 absorbing the water vapor is detached from the core 31 and is accommodated in the annulus 32. Meanwhile, the generated product gas 3 is discharged from the chamber 33 through the gas discharge portion 62 after leaving the core 31. Therefore, no separate device for separating the absorbent 82 from the catalyst 81 is required, and the reaction of the reaction gas 2, the water vapor absorption of the absorbent 82, ) Can be made at the same time. Further, according to the embodiment of the present invention, the reaction efficiency is high because the catalyst-absorbent fluidized bed is formed intensively in the core 31 and the reaction of the reaction gas 2 is concentrated in the core 31. [

According to one embodiment of the present invention, the reaction gas includes methanol (MeOH) and carbon dioxide (CO ₂ ). By the reaction of the reaction gas, a product gas and water vapor (H ₂ O) are produced. The product gas includes dimethylcarbonate (DMC). The catalyst 81 includes a copper-based catalyst or an iron-based catalyst. And the absorbent 82 comprises a metal oxide (MO). Therefore, the reaction occurring in the chamber 33 is expressed by the following reaction formula (1).

[Reaction Scheme 1]

2MeOH + CO ₂ = DMC + H ₂ O

The water vapor produced by Scheme 1 reacts with the metal oxide, which is the absorbent 82, to produce metal hydroxide.

The upper portion of the core 31 is opened to allow the absorbent 4 and the generated gas to escape. The upper portion of the core 31 is expanded more than the lower portion. Therefore, the flow rate of the catalyst 81 and the absorbent 82 is lower at the upper portion of the core 31 than at the lower portion. The absorbent 4 having a small density and / or a small size may be detached from the core 31 even if the flow velocity is slow at the top of the core 31. On the contrary, when the flow rate of the catalyst 81 is increased at the top of the core 31, the catalyst 81 having a large density and / or a large size is fixed in the core 31 under the influence of gravity. That is, the structure of the core 31 having the upper portion expanded can make the effect of fixing the catalyst 81 and releasing the absorbent 82 larger.

Specifically, the core 31 includes a core body 311 having an open upper portion and a core head 312 having upper and lower open portions and a lower portion coupled to an opened upper portion of the core body 311 . The supplied reaction gas 2 rises through the core body 311 and the core head 312. However, the core body 311 and the core head 312 are separated for the sake of convenience of explanation, and actually both may be integral. The core body 311 is cylindrical, but is not limited thereto, so that the supplied reaction gas 2 can rise uniformly. The core head 312 is an inverted conical shape, but is not limited thereto, so that the absorbent 4 absorbing water vapor easily escapes from the core 31.

The annulus 32 is an annular space located between the core 31 and the chamber 33. And the annulus 32 is an annular space surrounding the core 31. The dotted line shown in FIG. 2 distinguishes the annular 32 from the empty space above it. The absorbent 4 absorbing water vapor leaves the core 31 and drops down to the bottom of the annulus 32. The absorbent (5) that has fallen below the annulus (32) is discharged from the chamber (33). The regeneration reactor regenerates the discharged absorbent 5 and re-introduces the regenerated absorbent 11 into the chamber 33. The regenerating reactor will be described later.

The chamber 33 is cylindrical, but is not limited thereto, so that the reaction gas and the generated gas are smoothly dispersed therein. The chamber 33 provides an environment such as a temperature, a pressure and the like at which the reaction gas can react.

The gas supply unit 20 supplies the reaction gas 1 into the core 31 through the gas inlet 61. Accordingly, the gas supply unit 20 may include an air box. In addition, the gas supply unit 20 controls the supply rate of the reaction gas 1 so that the reaction gas 2 supplied into the core 31 rises at the first terminal speed. The reaction gas 2 having the first end velocity in the core 31 under the control of the gas supply unit 20 is supplied only to the catalyst 81 and the absorbent 82 of the absorbent 82 from the core 31 It can be released.

The absorbent 5 discharged from the chamber 33 passes through the first connection part 63 and flows into the transfer reactor 40. At this time, the first circulation pump 64 can transfer the absorbent 5 from the chamber 33 to the transfer reactor 40. However, the first circulation pump 64 may not be required depending on the operating environment. There may also be other means by which the absorbent 5 can be conveyed.

The fluidized gas (6) flows into the transfer reactor (40) through the gas inlet (65). In the transfer reactor (40), the absorbent and the fluidizing gas (7) rise together. The fluidized gas transports the absorbent in the state of absorbing water vapor in the transfer reactor (40). In particular, the solid absorbent is less fluid than the gas vapor, and the fluidized gas transports this absorbent to assist in the circulation of the absorbent. The fluidizing gas may be an inert gas or simply air.

The absorbent and fluidizing gas (8) are discharged to the top of the transfer reactor (40). The absorbent and the fluidizing gas 8 discharged from the transfer reactor 40 are introduced into the gas-solid separator 50 through the second connection part 66. At this time, the second circulation pump 67 can transfer the absorbent and the fluidizing gas 8 from the transfer reactor 40 to the gas-solid separator 50. However, the second circulation pump 67 may not be required depending on the operating environment. There may also be other means of transporting the absorbent and the fluidizing gas (8).

The gas-solid separator 50 separates the absorbent from water vapor. In the gas-solid separator 50, the absorbent that has absorbed water vapor becomes regenerated absorbent, and the water vapor absorbed in the absorbent becomes regenerated water. The regenerated water and the fluidizing gas (9) are discharged through the gas discharging portion (68). On the other hand, the regenerated absorbent 11 is reintroduced into the chamber 33 through the solid discharge portion 71. The regenerated absorbent 11 re-introduced into the chamber 33 can again absorb the water vapor in the chamber 33. [ Preferably, the regenerated absorbent 11 is reintroduced into the core 31 rather than the annuli 32. This is because reaction of the reaction gas intensively occurs in the core 31 rather than the annular 32, and the re-introduced regenerated absorbent can absorb a larger amount of water vapor for a unit time.

The gas-solid separator 50 can be, but is not limited to, a cyclone separator or a collision separator as is well known. Also, depending on the operating environment, the gas-solid separator 50 may be omitted or two or more gas-solid separators may be installed.

The condenser 69 condenses regenerated water discharged from the gas-solid separator 50 and passes the fluidized gas discharged from the gas-solid separator 50. The condensed water and the fluidizing gas (10) are discharged to the outside through the discharge portion (70).

[Example 2]

4 is a schematic view showing a circulation apparatus for separating catalyst fixing and absorbent according to an embodiment of the present invention. 4, the apparatus of Embodiment 1 is provided with a catalyst dispersing plate 34, an unreacted gas separator 72, a generated gas outlet portion 621, and a gas re-inlet portion 622 . The unreacted gas separator 72 is located outside the chamber 33. The gas discharge portion 62 connects the upper portion of the chamber 33 with the unreacted gas separator 72. The gas discharge portion 62 passes through the unreacted gas separator 72 and branches to the generated gas discharge portion 621 and the gas re-inlet portion 622. The gas re-inlet portion 622 connects the unreacted gas separator 72 and the lower portion of the chamber 33.

The catalytic dispersing plate 34 is annularly located in the annulus 32 and surrounds the lower portion of the core 31. The catalyst dispersing plate 34 includes a catalyst 81. The catalyst dispersing plate 34 may be composed of only the catalyst 81 and may be annular, and the catalyst 81 may be arranged and fixed in the annular structure. The catalyst dispersing plate 34 shown in FIG. 4 is of a porous type, but the catalyst dispersing plate 34 may be mesh-shaped or nozzle-shaped.

The generated gas 3 generated in the core 31 is discharged from the chamber 33 through the gas discharge portion 62 after leaving the core 31. However, the generated gas 3 may contain unreacted gas. This is because the supplied reaction gas 1 may not react in the core 31 at all. The unreacted gas separator 72 separates the unreacted gas from the discharged product gas 3. The separated unreacted gas 3b is reintroduced into the annulus 32 through the gas inlet 622 and the remaining generated gas 3a is discharged through the generated gas outlet 621 to the outside do.

The unreacted gas re-introduced into the annular 32 passes through the catalyst dispersion plate 34 and rises and is dispersed. At the same time, since the reaction environment is entirely formed in the chamber 33, the unreacted gas reacts. The catalyst 81 included in the catalyst dispersing plate 34 does not directly participate in the reaction of the unreacted gas but increases the reaction rate. The catalyst 81 included in the catalyst dispersing plate 34 may be firmly fixed to the bottom of the annulus 32.

However, the catalyst 81 included in the catalyst dispersing plate 34 may not be firmly fixed to the bottom of the annular 32. In this case, the re-introduced unreacted gas can flow the catalyst 81 contained in the catalyst dispersing plate 34. That is, a catalyst fluidized bed may be formed in the annular 32. However, in this case, the apparatus should be designed so that the catalyst 81 does not escape to the first connection portion 63.

4 may have a structure in which the catalyst 81 and the absorbent 82 can not be discharged from the chamber 33 unless the first circulation pump 64 is activated. In this case, regardless of whether the catalyst 81 contained in the catalyst dispersing plate 34 flows or does not flow due to the re-introduced unreacted gas, the catalyst 81 contained in the catalyst dispersing plate 34, (32).

The absorbent 4 absorbing water vapor in the core 31 and leaving the core 31 can be seated on the catalyst dispersion plate 34. Also, the absorbent 4 separated from the core 31 without absorbing water vapor in the core 31 can also be placed on the catalyst dispersion plate 34. The re-introduced unreacted gas reacts while passing through the catalyst dispersion plate 34 to generate the generated gas and steam. The water vapor generated here can be absorbed by the absorbent seated on the catalyst dispersion plate 34. Here, the absorption reaction of the absorbent may proceed while the absorbent flows in the annular 32. This is because the re-introduced unreacted gas can flow the absorbent seated on the catalyst dispersing plate 34 to form the absorbent fluidized bed in the annular 32. Of course, as described above, the catalyst 81 contained in the catalyst dispersing plate 34 can also flow together. On the other hand, the generated gas 3 generated by the reaction of the re-introduced unreacted gas is discharged from the chamber 33 through the gas discharge portion 62.

It is assumed that the apparatus shown in Figure 4 has a structure in which the catalyst 81 and the absorbent 82 can not be discharged from the chamber 33 unless the first circulation pump 64 is operated . It is assumed that the catalyst 81 contained in the catalyst dispersing plate 34 is not firmly fixed to the lower part of the annulus 32 and can be scattered by the re-introduced unreacted gas. Under these assumptions, the following process can be performed.

First, the re-introduced unreacted gas passes through the catalyst dispersion plate 34 and reacts to generate a generated gas and steam. Next, the unreacted gas generated in the annulus 32 and unreacted in the annulus 32 is discharged from the chamber 33. The water vapor generated in the annular 32 is absorbed by the absorbent placed on the catalyst dispersing plate 34. Next, the first circulation pump 64 may be operated. At this time, the first circulation pump 64 is operated at a speed (hereinafter referred to as " second end velocity ") at which the adsorbent is discharged from the chamber 33 and the catalyst 81 of the catalyst dispersion plate 34 is not discharged , The absorbent can be pumped. Accordingly, the catalyst 81 of the catalyst dispersing plate 34 is fixed to the annular 32, and the absorbent can be discharged, regenerated, and re-injected.

From Example 2, the following facts are confirmed.

First, since the unreacted gas is re-introduced and reacted through the catalyst dispersion plate 34, the reaction gas is not wasted and the process efficiency is high.

Secondly, since the reaction gas is reacted not only in the core 31 but also in the annulus 32, the entire space in the chamber 33 is efficiently utilized.

Third, according to one embodiment, the absorbent desorbed from the core 31 is placed on the catalyst dispersing plate 34, and the unreacted gas passes through the catalyst dispersing plate 34 on which the absorbent is placed. That is, water vapor is absorbed not only in the core 31 but also in the annulus 32. Therefore, it is not necessary to add the absorbent for absorbing the water vapor generated in the annulus 32 to the annular 32, and the process efficiency is high.

Fourthly, according to one embodiment, since the first circulation pump 64 discharges the absorbent in the annulus 32 from the chamber 33 at the second terminal speed, not only the core 31, In the cannula 32, the catalyst is fixed and the absorbent is separated. Therefore, the apparatus of the second embodiment has higher process efficiency than the apparatus of the first embodiment, and can prevent the catalyst from being inferior in activity, abrasion, and contamination to the same level as in the first embodiment.

[Example 3]

In Fig. 2, except for the condenser 69 and the discharge portion 70, the catalyst fixing and absorbent separation and circulation apparatus of Embodiment 3 is obtained. In Example 3, the reaction gas reacts in the core 31 to produce the produced gas and carbon dioxide. The absorbent absorbs the generated carbon dioxide and is released, circulated, regenerated, and reintroduced. The carbon dioxide and the fluidizing gas 9 regenerated from the gas-solid separator 50 are discharged to the outside through the gas discharge portion 68. That is, the third embodiment is the same as the first embodiment except that the kind of the reaction gas, the kind of the generated gas, the water vapor is changed to the carbon dioxide, and the gas is not condensed.

According to one embodiment of the present invention, the reaction gas comprises methane (CH ₄ ) and water (H ₂ O). The reaction gas reacts to generate a product gas and carbon dioxide (CO ₂ ). The product gas includes hydrogen (H ₂ ). The catalyst 81 includes a copper-based catalyst or an iron-based catalyst. And the absorbent 82 comprises a metal oxide (MO). Therefore, the reaction occurring in the chamber 33 is as shown in the following reaction formula (2).

[Reaction Scheme 2]

CH ₄ + 2 (H ₂ O) = 4H ₂ + CO ₂

The carbon dioxide produced by scheme 2 reacts with the metal oxide, which is the absorbent 82, to produce metal carbonates.

[Example 4]

In Fig. 4, except for the condenser 69 and the discharge portion 70, the catalyst fixing and absorbent separation and circulation apparatus of Embodiment 4 is obtained. In Embodiment 4, the reaction gas reacts in the core 31 to produce the generated gas and carbon dioxide. The absorbent absorbs the generated carbon dioxide and is released, circulated, regenerated, and reintroduced. The carbon dioxide and the fluidizing gas 9 regenerated from the gas-solid separator 50 are discharged to the outside through the gas discharge portion 68. That is, the fourth embodiment is the same as the second embodiment except that the kind of the reaction gas, the kind of the generated gas, the vapor is changed to carbon dioxide, and the gas is not condensed. The difference between Example 2 and Example 4 was explained in Example 3. [

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 embodiments, but, on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims. will be. Therefore, the true scope of the present invention should be defined by the appended claims.

20: gas supply part
30: core-annular reactor
31: Core
311: Core body
312: core head
32: Anunla
33: chamber
34: catalyst dispersion plate
40: Transfer reactor
50: gas-solid separator
81: Catalyst
82: Absorbent

Claims (31)

A core which receives the catalyst and the absorbent, receives the reaction gas into the inside thereof and has an open top;
A chamber for receiving the core; And
A space located between the core and the chamber, the annulus surrounding the core,
In the core, the supplied reaction gas flows through the received catalyst and the absorbent to produce a product gas and water vapor;
The generated water vapor is absorbed by the flowing absorbent;
Said absorbent absorbing said water vapor escapes said core through said open top and is received in said annular;
Wherein the catalyst is fixed within the core.
The method according to claim 1,
Wherein the generated product gas leaves the core through the open top and exits the chamber.
The method according to claim 1,
Wherein the absorbent contained in the annulus is withdrawn from the chamber, regenerated and then reintroduced into the chamber.
The method according to claim 1,
And a gas supply unit for supplying the reaction gas into the core.
5. The method of claim 4,
Wherein the gas supply unit controls the supply rate of the reaction gas so that the catalyst is fixed in the core and only the absorbent that has absorbed the water vapor leaves the core.
The method of claim 3,
Further comprising a regeneration reactor for regenerating the absorbent discharged from the chamber after absorbing the water vapor and re-introducing the regenerated absorbent into the chamber.
The method according to claim 6,
Wherein the regenerating reactor comprises a transfer reactor in which the absorbent and the fluidizing gas that have been discharged from the chamber after absorbing the water vapor are introduced and which discharges the introduced absorbent and the fluidizing gas, .
8. The method of claim 7,
Wherein the fluidizing gas is an inert gas or air.
8. The method of claim 7,
Wherein the fluidizing gas transfers the introduced absorbent in the transfer reactor.
8. The method of claim 7,
The regeneration reactor further comprises a gas-solid separator for introducing the absorbent and the fluidizing gas discharged from the transferring reactor, discharging regenerated water and fluidizing gas, and recycling the regenerated absorbent into the chamber And a circulation device for separating the catalyst fixing and absorbent.
11. The method of claim 10,
Wherein the gas-solid separator is a cyclone separator or an impingement separator.
[12] has been abandoned due to the registration fee. 11. The method of claim 10,
Wherein the regenerating reactor further comprises a condenser connected to the gas-solid separator to condense the discharged regenerated water to discharge the condensed water and to pass the discharged fluidized gas. Separate circulation device.
The method according to claim 1,
Wherein the open top of the core is inverted cone-shaped.
The method according to claim 1,
Wherein the reaction gas comprises methanol and carbon dioxide.
The method according to claim 1,
Wherein the catalyst comprises a copper-based catalyst or an iron-based catalyst.
The method according to claim 1,
Wherein the catalyst fixed in the core is denser than the absorbent.
The method according to claim 1,
Wherein the catalyst fixed within the core is larger in size than the absorbent.
The method according to claim 1,
Wherein the absorbent comprises a metal oxide. ≪ RTI ID = 0.0 > 15. < / RTI >
A core which receives the catalyst and the absorbent, receives the reaction gas into the inside thereof and has an open top;
A chamber for receiving the core;
An annulus surrounding the core, the annular space being located between the core and the chamber; And
A catalytic dispersion plate disposed in the annulus and surrounding the bottom of the core,
In the core, the supplied reaction gas flows through the received catalyst and the absorbent to produce a product gas and water vapor;
The generated water vapor is absorbed by the flowing absorbent;
Said absorbent absorbing said water vapor escapes said core through said open top and is received in said annular;
Wherein the catalyst is fixed within the core.
20. The method of claim 19,
Wherein the generated product gas leaves the core through the open top and exits the chamber.
21. The method of claim 20,
And the unreacted gas in the discharged product gas is reintroduced into the annunla.
22. The method of claim 21,
Further comprising an unreacted gas separator for separating the unreacted gas from the discharged product gas so that the unreacted gas is reintroduced.
22. The method of claim 21,
And the re-introduced unreacted gas passes through the catalyst dispersion plate so as to be dispersed while being reacted.
24. The method of claim 23,
Wherein the absorbent leaving the core rests on the catalyst dispersion plate located in the annulus.
20. The method of claim 19,
Wherein the absorbent contained in the annulus is withdrawn from the chamber, regenerated and then reintroduced into the chamber.
20. The method of claim 19,
Wherein the catalyst dispersion plate is of a porous, mesh, or nozzle type.
A core which receives the catalyst and the absorbent, receives the reaction gas into the inside thereof and has an open top;
A chamber for receiving the core; And
A space located between the core and the chamber, the annulus surrounding the core,
In the core, the supplied reactant gas flows the absorbing agent and the accommodated catalyst to produce a product gas and carbon dioxide;
The generated carbon dioxide is absorbed by the flowing absorbent;
The absorbent absorbing the carbon dioxide leaves the core through the open top and is received in the annulus;
Wherein the catalyst is fixed within the core.
[Claim 28 is abandoned upon payment of registration fee.] 28. The method of claim 27,
Wherein the reaction gas comprises methane and water.
28. The method of claim 27,
Wherein the absorbent contained in the annulus is withdrawn from the chamber, regenerated and then reintroduced into the chamber.
A core which receives the catalyst and the absorbent, receives the reaction gas into the inside thereof and has an open top;
A chamber for receiving the core;
An annulus surrounding the core, the annular space being located between the core and the chamber; And
A catalytic dispersion plate disposed in the annulus and surrounding the bottom of the core,
In the core, the supplied reactant gas flows the absorbing agent and the accommodated catalyst to produce a product gas and carbon dioxide;
The generated carbon dioxide is absorbed by the flowing absorbent;
The absorbent absorbing the carbon dioxide leaves the core through the open top and is received in the annulus;
Wherein the catalyst is fixed within the core.
31. The method of claim 30,
Wherein the absorbent contained in the annulus is withdrawn from the chamber, regenerated and then reintroduced into the chamber.

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