Patent Application
20150174546
The present invention relates to a flow velocity variable type fluidized bed reactor, and more specifically to a flow velocity variable type fluidized bed reactor which is capable of maintaining smooth transfer of solid particles by varying flow velocity in the fluidized bed reactor while increasing concentration of a gaseous reactant with respect to the solid particles.
Conventionally, a carbon dioxide (CO2) capturing system employs a wet process to recover CO2. That is, the wet process is carried out by passing CO2-containing gas through an amine solution, to allow CO2 to be absorbed into the solution and regenerating the solution in a regeneration column, thus reusing the solution. However, the wet process has a demerit of further generating waste water during an operation of the wet process.
In order to overcome disadvantages of the wet process, a dry process for recovering CO2 has been proposed in the art. A system using the dry method is configured to recover CO2 by using two reactors, wherein CO2 fed into a absorption reactor is adsorbed to a solid absorbent (a dry absorbent) and removed. The solid absorbent inflows into a regeneration reactor (regenerator′) to remove the adsorbed CO2, H2O is adsorbed to the solid absorbent in a pre-treatment reactor, and then the solid absorbent is recycled to the absorption reactor.
However, as illustrated in
In particular, when using a fluidized bed reactor as the absorption reactor, the partial pressure of exhaust gas is lowered toward the upper side of the absorption reactor (see
Accordingly, the conventional method has a problem that the absorption rate of CO2 by the absorption reactor cannot increase any more.
In consideration of the above-described circumstances, it is an object of the present invention to provide a flow velocity variable type fluidized bed reactor which is capable of maintaining smooth transfer of solid particles by varying flow velocity in the fluidized bed reactor while increasing concentration of a gaseous reactant with respect to the solid particles.
In order to accomplish the above objects, there is provided a fluidized bed reactor in which solid absorbents and reaction gases inflow to cause chemical reaction between the solid absorbents and reaction gas in a fluidized state, including: a lower high-speed unit into which the solid particles and the liquid particles inflow; a middle low-speed unit which is connected to an upper end portion of the lower high-speed unit, and is configured to decrease a flow velocity therein to be lower than the lower high-speed unit; and an upper high-speed unit which elongates from an upper end of the middle low-speed unit, and is configured to increase the flow velocity therein to be greater than the middle low-speed unit.
Herein, the lower high-speed unit may have a smaller cross-sectional area than the middle low-speed unit, and the upper high-speed unit may have a smaller cross-sectional area than the middle low-speed unit.
In addition, the upper high-speed unit may have a cross-sectional area gradually decreased toward an upper end thereof.
Further, the reaction gases may be additionally supplied to the middle low-speed unit.
Further, the lower high-speed unit may have an extension part integrally formed at an upper end thereof, and the extension part may be disposed inside of the middle low-speed unit, and the additionally supplied reaction gases may be introduced into a lower position than an upper end of the extension part.
According to the present invention, even when the height of the solid particles having the same flow rate is increased, the reaction may actively occur due to an increase in the concentration of the reaction gases by additionally supplying the reaction gases, and the flow velocity at the position where the reaction gases are additionally supplied may adjust so as to be equal to or larger than that of the lower high-speed unit. Further, after ending of the reaction, the mixture of the gas and the solid particles may be smoothly transferred by again increasing the fluid velocity.
Hereinafter, preferable embodiments of the present invention will be described with reference to the accompanying drawings. Referring to the drawings, wherein like reference characters designate like or corresponding parts throughout the several views. In the embodiments of the present invention, a detailed description of publicly known functions and configurations that are judged to be able to make the purport of the present invention unnecessarily obscure are omitted.
The fluidized bed reactor 102 has a configuration whose cross-sectional area is changed twice from a lower portion toward an upper side, unlike a conventional regenerator. That is, the fluidized bed reactor 102 includes a lower high-speed unit 150 into which solid particles and liquid particles inflow, a middle low-speed unit 152 which is connected to an upper end portion of the lower high-speed unit 150, and is configured to decrease the flow velocity therein to be lower than the lower high-speed unit 150, an upper high-speed unit 154 which elongates from an upper end of the middle low-speed unit 152, and is configured to increase the flow velocity therein to be greater than the middle low-speed unit 152.
In the lower high-speed unit 150, since the solid particles and reaction gases, which are not yet reacted while being fluidized, are present, a sufficient reaction may occur under a high flow velocity condition.
In addition, when the solid particles and reaction gases reach the upper side of the lower high-speed unit 150, a concentration of reactants contained in the reaction gases is lowered by a reaction in the lower high-speed unit, and thereby the reaction slowly occurs even when the solid particles still having reaction capability are present therein.
Therefore, in the present invention, the middle low-speed unit 152 configured to decrease the flow velocity therein to be lower than the lower high-speed unit 150 is disposed to the upper side of the lower high-speed unit 150. By this, if the flow velocity therein is decreased in the middle low-speed unit, contact time between the reaction gases and the solid particles is increased, so that sufficient reaction may occur therein even when the reaction velocity is slow. Therefore, most of the solid particles exhaust their reaction capability during passing through the middle low-speed unit 152. In the first embodiment of the present invention, the middle low-speed unit 152 is configured to decrease the flow velocity therein by having a larger cross-sectional area than the lower high-speed unit 150 (a1<a2).
However, when fluidization does not occur due to a decrease in the flow velocity, or the concentration of the reaction gas is low in spite of an increase in the pressure, it is possible to additionally supply the reaction gases to the middle low-speed unit 152. By this, the concentration of the reaction gas may be increased in the middle low-speed unit 152. However, when the flow rate of the added reaction gases is significantly increased, a fluidization phenomenon wherein the fluids move upward from the lower high-speed unit 150 by an air curtain effect may occur, and therefore an effect obtained by installing the middle low-speed unit 152 may be decreased.
Accordingly, it is preferable to avoid direct contact between the additionally supplied reaction gases and the solid particles. For this, as illustrated in
When additionally supplying the reaction gases, it is possible to supply the reaction gases to a portion at which the middle low-speed unit 152 and the lower high-speed unit 150 are connected with each other. The upper high-speed unit 154 is disposed at the upper side of the middle low-speed unit 152 to increase the flow velocity therein, so that the reacted solid particles and the residual gas easily move to a subsequent process. For this, in the first embodiment of the present invention, the upper high-speed unit 154 is formed to have a smaller cross-sectional area than the middle low-speed unit 152 (a2<a3).
As illustrated in
Herein, it is preferable that the flow velocity in the upper high-speed unit 154 is at least equal to or larger than that of the lower high-speed unit 150.
A length (b1) of the lower high-speed unit 150, a length (b2) of the middle low-speed unit 152, and a length (b3) of the upper high-speed unit 154 may be suitably selected depending on the type, flow rate and reaction velocity of the reaction gases and the solid particles.
The fluidized bed reactor 102 according to the first embodiment of the present invention basically has the above described configuration. Next, a dry carbon dioxide (CO2) capturing device 100 including the fluidized bed reactor 102 will be described with reference to
The dry CO2 capturing device 100 includes the fluidized bed reactor 102 according to the first embodiment of the present invention, a fluidized bed cyclone 110, a regenerator 114 and a pre-treatment reactor 120. The pre-treatment reactor 120 basically has the same structure as the regenerator 114, but regenerated gas is supplied to the regenerator 114, while pre-treatment gas is supplied to the pre-treatment reactor 120.
The fluidized bed reactor 102 includes exhaust gas supply lines 106 and 108 which are respectively connected to the lower high-speed unit 150 and the middle low-speed unit 152 to supply exhaust gases of the reaction gases. The exhaust gas supply lines 106 and 108 include control valves 130 and 132 installed therein, and are connected to an exhaust gas supply source (not illustrated) through a main supply line 134. As described above, the exhaust gas supply line 108 connected to the middle low-speed unit 152 is disposed at the lower position of the upper end of the extension part 156.
Dry solid absorbent of the solid particle used in the dry CO2 capturing device 100 may use any absorbent commonly used in the related art, and in particular, K2CO3 or Na2CO3 having favorable CO2 adsorption is preferably used.
The fluidized bed cyclone 110 is an apparatus commonly known in the art, wherein the solid absorbent containing CO2 absorbed therein (‘CO2-absorbed solid absorbent’) in the fluidized bed reactor 102 is centrifuged to cause the solid absorbent to fall down by self-weight while light gas, that is, the exhaust gas free from CO2 may flow through an isolated gas discharge line 112 connected to the fluidized bed cyclone 110 to further operations.
The regenerator 114 heats the CO2-absorbed solid absorbent to allow the solid absorbent to release CO2. Herein, a heating temperature of the solid absorbent is higher than the injection temperature of the exhaust gas. Heating the solid absorbent in the regenerator 114 is performed in a fluidized state by the regenerated gas inflowing from a regenerated gas supply line 116, wherein the regenerated gas may use steam. When using steam as the regenerated gas, removing moisture only from the regenerated gas may preferably provide pure CO2. Then, the solid absorbent moves to the pre-treatment reactor 120 through am absorbent outlet line 122 connected to the regenerator 114.
The regenerator 114 may further include a regeneration cyclone 118 connected thereto so as to prevent loss of the solid absorbent suspended by the regenerated gas. The regeneration cyclone 118 may substantially have the same structure as that of the fluidized bed cyclone 110. Gas absorbed to the solid absorbent, i.e., CO2 is discharged through a CO2 discharge line 117 connected to the regeneration cyclone 118.
The solid absorbent passed through the regenerator 114 may have a temperature, at which CO2 is easily absorbed in the pre-treatment reactor 120, and then, move to the fluidized bed reactor 102.
In order to cool the solid absorbent in the pre-treatment reactor 120, a pre-treatment gas is supplied thereto through a pre-treatment gas supply line 124. Such a pre-treatment gas may include, for example, air or inert gas such as nitrogen. A temperature of the pre-treatment gas should be at least equal to or less than the injection temperature of the exhaust gas fed to the fluidized bed reactor 102. In addition, the pre-treatment gas may rapidly cool the solid absorbent by fluidized bed motion of the solid absorbent in the pre-treatment reactor 120.
In addition, the dry solid absorbent containing H2O absorbed therein has a characteristic in which CO2 is easily soluble in H2O, and may hence increase CO2 absorption rate. Accordingly, it is preferable to supply the pre-treatment gas in a saturated water vapor state so as to early moisturize the solid absorbent.
The pre-treatment reactor 120 may include a pre-treatment cyclone 126 connected thereto to prevent the solid absorbent from being removed. Accordingly, the solid absorbent recovered by the pre-treatment cyclone 126 is fed back again to the pre-treatment reactor 120, while only the pre-treatment gas with absorbed thermal energy may be discharged through a pre-treatment gas discharge line 127. The solid absorbent discharged from the pre-treatment reactor 120 by contacting the pre-treatment gas with the solid absorbent should be controlled so as to have a temperature substantially identical to the injection temperature of the fluidized bed reactor 102.
Next, a fluidized bed reactor 104 according to a second embodiment of the present invention will be described with reference to
While the present invention has been described with reference to the preferred embodiments, the present invention is not limited to the above-described embodiments, and it will be understood by those skilled in the related art that various modifications and variations may be made therein without departing from the scope of the present invention as defined by the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10-2012-0054667 | May 2012 | KR | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/KR2013/004446 | 5/21/2013 | WO | 00 |
