TW201023969A - Adsorbent, regenerative cycle operation of the same and apparatus of regeneration the same - Google Patents

Abstract

An adsorbent is provided. The adsorbent includes metal oxide having porous with pore diameter of 0.1 nm to 100 nm, the specific surface of 0.5 to 38.28 cm<SP>2</SP>/g and the adsorption capacity of 0.25g CO2/1g metal oxide.

Description

IW 29621twf.doc/n 201023969 IX. Description of the Invention: [Technical Field of the Invention] The present invention relates to an adsorbent, a method for recycling the same, and a regenerating device thereof. ^ [Previous Technology] The Intergovernmentg ❹ Panel on Climate Change (IPCC) showed in the 2001 Western Science Assessment Report that if CO2 emissions maintain current emissions levels, they will be global to Xiqiao in 2100. The average ambient temperature will rise by 14 to 5.8 degrees Celsius. This rapid warming has never been seen in the past millennium, and this result will cause sea levels to rise by 9 to 88 cm. From the point of view of climate change, 'this is the biggest increase in the past - the past year, the current temperature is only 4 degrees Celsius from the last ice age, and the last lpcc 1995 assessment report 摄 5 degrees to 3 degrees Celsius Compared with the temperature increase of 1.4 to 5.8 degrees Celsius, the predicted results should be shocking. The meteorological disasters of the extended ® must also be severe. The IPCC 2001 report predicts that meteorological disasters caused by global warming will result in more than $300 billion in annual losses. Therefore, reducing carbon dioxide in the atmosphere is a common problem that human beings must face and need to solve quickly. Big problem. SUMMARY OF THE INVENTION The present invention provides an adsorbent that can effectively adsorb dioxide. The invention provides a method for manufacturing an adsorbent, which can reduce the energy consumption of the energy consumption of the 2010A 129, which is 1A W 2962 ltwf, doc/n loss. The present invention provides a method of regenerating a sorbent which regenerates the adsorbent in an easy process. The apparatus of the present invention &amp; for a regenerative adsorbent is simple in equipment and low in cost. The invention provides an adsorbent comprising a metal oxide having a plurality of pores having a diameter of from 0.1 nm to 100 nm, and a specific surface area of 0^2 38 28 • m ^ 2 /g of adsorbed amount of at least 0.25 g of carbon dioxide /1 gram of metal oxide. According to an embodiment of the present invention, the conversion rate of the above adsorbent is at least 0.3, and the cycle of adsorbing and desorbing carbon dioxide at least 1 time can be repeated. According to the present invention, in the above adsorbent, the metal oxide includes an oxide of an alkaline earth element, an oxide of an alkali gold element, or a mixture thereof. According to an embodiment of the invention, the adsorbent further comprises a metal hydroxide, wherein the content of the metal oxide is 40% by weight to 80% by weight, and the content of the cerium metal hydroxide is 20% by weight [~6〇 weight %. According to an embodiment of the present invention, in the above adsorbent, the metal hydroxide compound includes a hydroxide of a soil member element or a hydroxide of an alkali gold group element or a mixture thereof. The adsorbent according to the embodiment of the present invention further comprises a metal carbonic acid compound wherein the content of the metal oxide is from 75% by weight to 95% by weight. The content of the metal carbonate compound is from 5% by weight to 25% by weight. According to the embodiment of the present invention, the above adsorbent, metal carbonic acid 201023969

1W 29621twf.doc/n The compound includes a carbonate compound of an alkaline earth element, a carbonic acid compound of an alkali gold group element, or a mixture thereof. According to the embodiment of the present invention, in the adsorbent, the adsorbent further comprises a metal hydroxide and a metal carbonate compound, wherein the content of the metal oxide is 30% by weight to 75% by weight, and the content of the metal hydroxide is 20%. The weight % to 50% by weight and the content of the metal carbonate compound are 5% by weight to 25% by weight. The present invention further provides a method of regenerating a sorbent comprising providing a metal oxide-containing adsorbent which has adsorbed the oxidized complex. Then, the adsorbent is subjected to a calcining process in an environment containing saturated steam and at least one gas to regenerate the adsorbent. Thereafter, carbon dioxide is adsorbed by the regenerated adsorbent. In the method of the regeneration cycle of the adsorbent described above, the metal oxide includes an oxide of an alkaline earth element, an oxide of an alkali gold element, or a mixture thereof. In the method of the regeneration cycle of the adsorbent described above, the volume ratio of saturated water vapor to gas (saturated water vapor/gas) is between 2 and 20, in accordance with an embodiment of the present invention. According to an embodiment of the present invention, the flow rate of the saturated steam in the regeneration cycle of the adsorbent described above is 165 to 1650 ml/min. According to the embodiment of the present invention, the flow rate of the gas in the regeneration cycle of the adsorbent described above is 8.25 to 825 ml/min. In the method of the regeneration cycle of the adsorbent described above in the embodiment of the present invention, the gas includes nitrogen gas or a mixed gas thereof. According to the embodiment of the present invention, in the method for regenerating the adsorbent, the temperature of the calcination process is 25 (rc~1〇〇〇t), according to the embodiment of the present invention, the adsorption is as described above. In the method of regeneration cycle of the agent, the maintenance time of the calcination process is 1 〇 to 4 〇 minutes.

According to the embodiment of the present invention, in the method of regenerating the adsorbent described above, the dance X firing process is carried out under normal pressure. The present invention further provides an apparatus for regenerating a composition of a sorbent comprising a reactor, a temperature control device, a steam generating device, a gas supply device, and a vapor separation device connected to the reactor. The reactor is used to administer the adsorbent 2 to which carbon dioxide has been adsorbed. A temperature control device is used to control the temperature of the reactor. A steam generating device is used to supply saturated steam to the reactor. A gas supply means is used to supply at least one gas to the reactor. A vapor separation unit is used to separate the saturated water vapor and gas discharged from the reactor.

- oxidizing carbon, helium, neon, argon, according to an embodiment of the present invention, in the apparatus for regenerating the adsorbent composition, the reactor comprises a fixed bed type, a fluidized bed type, a disturbed bed type or a high temperature resistant furnace. . In the apparatus for regenerating the adsorbent composition described above in accordance with an embodiment of the present invention, the vapor separation device comprises a vapor condensation device and a flow meter. The present invention provides a sorbent composition having a sufficiently large pore size and a high specific surface area, so that the sorbent composition of the present invention has a relatively high adsorption amount and can be repeatedly adsorbed and desorbed multiple times and has When the conversion rate is high, carbon dioxide can be effectively adsorbed. 201023969 ---------*1W 29621twf.doc/n The method of the regeneration cycle of the adsorbent of the present invention can reduce energy loss and save cost. The method of regenerating the adsorbent of the present invention can be prepared in a simple process. The apparatus for regenerating an adsorbent of the present invention is simple in equipment, easy to obtain, and low in cost. The above described features and advantages of the present invention will become more apparent from the following description. [Embodiment] Metal oxides have an adsorption property and are currently used to capture carbon monoxide in smoke. After adsorbing carbon dioxide with a metal oxide-containing adsorbent, the metal oxide in the adsorbent will react with carbon dioxide to form a metal carbonate compound. The metal carbonate compound (mco3) is at a high temperature (25 (TC~1000.) calcined to regenerate metal oxides (MO) and carbon dioxide. According to this phenomenon, carbon dioxide can be captured and separated. Compressed in the earth's crust or chemically reacted with serpentine (Mg3Si205(OH)4) to form a stable mineral stone, as shown in the following formula:

Mg3Si205(0H)4+ 3C02(g) 3MgC03 + 2Si02 +2H20(1) -63.6 kJ/mole C02 Taking calcium oxide (CaO) as an example, its chemical stability is high, and it has high absorption after repeated use. active. CaO captures the absorption load of carbon dioxide, theoretically up to 0.7857 grams (: 02^g0&amp;0, but actually in the sense of 29621twf.doc/n 201023969,w

3lW thinks about 0.393g CCyi gram CaO compared to other chemical absorbents (0.06g C02/1g monoethanolamine (MEA), 〇〇88g c〇2/1g active disgusting' 0132g C〇2/l In the case of silica gel, it can absorb more carbon dioxide with a small amount of absorption. Moreover, calcium oxide can directly separate carbon dioxide in the flue gas environment, compared with the sulfur-free oxide (SOx) interference without the traditional absorption procedure, but can remove SOx at high temperature and treat carbon dioxide in the flue gas. Low concentration, can produce carbon monoxide of pure purity during regeneration. In addition, there is no hazardous material present, and CaO (lime) and CaC〇3 (slaked lime) are much safer than other chemical absorbents. On the other hand, the equipment for capturing carbon dioxide by calcium oxide is simple and has a large amount of processing. Although there is no commercialization at present, the independent operation of each part has already been operated by large units in the industrial sector, and commercialization is easier. However, CaO has a tendency to slowly decrease after repeated use, so it is necessary to add fresh CaO from time to time to compensate for the loss. Although 'CaO is cheap and the production area can be mass-produced and easy to obtain, fresh CaO can be added to compensate for the loss. However, if the Φ CaO can be modified by a simple procedure, the speed of activity reduction can be greatly reduced. Capture costs. In order to modify the metal oxide, the speed of the activity is reduced. The present invention uses not only high temperature (250 ° C ~ 1000 ° C) heating, but also heating during the regeneration of the adsorbed carbon dioxide adsorbent. Also supplied with saturated steam and a gas such as nitrogen, carbon dioxide, helium, neon, argon or a mixture thereof at normal pressure (the "normal pressure" as used herein means atmospheric pressure or ±10%) Pressure) for calcination. 9 201023969

JI W 29621 twf.doc/n In more detail, the method of the embodiment of the present invention can be applied to an adsorbent which has adsorbed carbon dioxide, and a metal carbonate compound may be formed after the metal oxide in the adsorbent adsorbs carbon dioxide. The metal carbonate compound is, for example, a carbonic acid compound of a soil member element or a carbonic acid compound of a gold group element or a mixture thereof. The carbonic acid compound of the soil member element is, for example, magnesium carbonate or carbonic acid. The carbonic acid compound of the alkali gold group element is, for example, sodium carbonate or potassium carbonate. When the adsorbent having adsorbed carbon dioxide is calcined, the temperature increase rate is controlled to reach the set calcination temperature. After reaching the set calcination temperature, it is maintained at normal pressure, and the calcination is maintained for a period of time according to the type of different metal oxides, so that the metal carbonate compound in the adsorbent adsorbing carbon dioxide is sufficiently reacted with saturated water vapor and gas. Forming a metal oxide having an improved adsorption and desorption of an emulsified carbon to achieve the purpose of regeneration of the adsorbent. In the calcination process, the flow rate of the saturated steam introduced is, for example, 165 to 1650 ml/min g; the flow rate of the gas is, for example, 8 25 to 825 ml/min. In one embodiment, the volume ratio of saturated steam and gas (saturated spa steam/gas) is controlled, for example, between 2 and 20. In another embodiment, the volume ratio of saturated steam and gas (saturated water vapor/gas) is controlled, for example, between 6 and 14. The temperature increase rate is, for example, 25 to 4 〇〇 c / minute, and the speed is brought to the set calcination temperature. The calcination temperature varies depending on the kind of the adsorbent, and is usually, for example, at 25 Torr. 〇~1〇〇〇. Hey. After reaching the set calcination temperature, the time for maintaining the calcination is, for example, 丨 minute to 600 minutes. In one embodiment, the adsorbent contains calcium oxide, which forms calcium carbonate after adsorbing carbon dioxide, and the calcination temperature is, for example, 75〇°c~95〇201023969-------&gt; JW 29621twf.doc/n C, The time for maintaining the calcination is 1 minute to 4 minutes. In another embodiment, the adsorbent contains magnesium oxide, which forms carbonic acid after adsorbing carbon dioxide, and the calcination temperature is, for example, 50 (rc~70 (rc' maintains the calcination time of 10 minutes to 40 minutes. The adsorbent contains a metal oxide such as an oxide of an alkalinium earth element or an oxide of an alkali gold group element or a mixture thereof, and an oxide of the alkaline earth element is, for example, magnesium oxide or calcium oxide. • The oxide of the group element is, for example, sodium oxide or potassium oxide. The metal oxide has a plurality of pores, and the diameter of the pore is, for example, 01 nm to 100 nm, and the specific surface is 0.5 to 38.28 m ^ 2 /g. When the adsorbent adsorbs carbon dioxide again, its adsorption amount can reach at least 25 grams of carbon dioxide and 8 grams of metal oxide, and can be repeatedly sucked and desorbed for at least 1 cycle, and the conversion rate can be at least 0.3. The shape of the regenerated adsorbent It may be in the form of granules or powder. In addition, the regenerated adsorbent may include, in addition to the metal oxide, residual metal carbonate or metal hydroxide. The regenerated adsorbent 括 comprises a metal oxide and a residual metal carbonate compound, or includes a metal oxygen compound and a metal hydroxide, or includes a metal oxide, a residual metalloid acid compound, and a metal hydroxide. The remaining metal carbonate compound is, for example, a carbonic acid compound of a soil group element or a gold group element or a mixture thereof. The carbonic acid compound of the alkaline earth element is, for example, magnesium carbonate or calcium carbonate, etc. The carbolic acid compound of the gold group element is, for example, sodium carbonate or Potassium acid sulphate, etc. The adsorbent metal hydroxide is, for example, an earthworm or a gold component of a gold group element or a mixture thereof. In one embodiment, the particulate adsorbent pack 11 201023969 iW 29621twf.doc/n 75%~95% metal oxide and 5%~25% metal carbonic acid compound. In another embodiment, the granular adsorbent comprises 40%~80% metal oxide and 20%~60% metal In another embodiment, the particulate adsorbent comprises 30% to 75% metal oxide, 20% to 50% metal cerium oxide, and 5% to 25% metal carbonic acid compound. Said "%" means weight percent. Figure 1 is an apparatus for preparing an adsorbent according to an embodiment of the present invention. The apparatus 100 includes a reactor 10, a temperature control device 12, a steam generating device 14, and a gas. The supply device 16 and the steam separation device 18. The adsorbent 10 is used to place the adsorbent having adsorbed carbon dioxide in the reactor 10. The reactor 10 may be a fixed bed type, a fluidized bed type, a disturbed bed type or a high temperature resistant furnace. The steam generating device 14 and The reactors 10 are connected by a tube for supplying saturated water vapor to be introduced into the reactor 10 to react with the adsorbent which has adsorbed carbon dioxide. The gas supply device 16 and the reactor 1 are connected by a pipe. 'To supply nitrogen, carbon dioxide, helium, neon, argon or a mixture thereof to the reactor 10 to react with the adsorbent which has adsorbed carbon dioxide. The saturated water vapor supplied by the steam generating device 14 and the gas supplied from the gas supply device 16 may be respectively introduced into the reactor 1 (as shown by the broken lines 24a and 24b) or may be passed into the reactor. Mix before 1〇 (as shown by the solid lines 26a and 26b). In order to effectively control the flow rate of saturated water vapor or gas introduced into the reactor 10, a control valve member (not shown) may be provided on the pipe member. The temperature control device 12 is configured to control the temperature of the reactor 10 to cause the adsorbent having adsorbed carbon dioxide in the reactor 10 and the saturated water vapor to be passed in the appropriate temperature environment to be 12 201023969 lW 29621 twf.doc/n and Gas reaction. The vapor separation unit 18 is connected to the reactor 10 by means of a tube for removing saturated water vapor and gas discharged from the reactor 10. In one embodiment, when the reaction is carried out, the saturated water vapor and the pressure of the gas are greater than the normal pressure, and the saturated water vapor at a normal pressure in the reactor 10 and the gas are discharged through the steam separation device due to the positive pressure. The steam separation unit 18 may include a pump, such as a steam condensing unit 20 and a flow meter 22, to achieve the desired efficiency. The steam condensing unit 20 can be used to condense the saturated water vapor discharged from the reactor 10, and the flow meter 22 can measure the reactor 1'. The discharged gas and the saturated water vapor which cannot be condensed by the steam condensing unit 20 flow. Since the method for regenerating the adsorbent of the present invention can be carried out under normal pressure, the system does not need to maintain a vacuum, and therefore, the loss of energy can be reduced. Furthermore, 'because the present invention only needs to use saturated steam and gas for calcination, and the temperature of calcination can be carried out at a lower temperature, without using superheated steam' and without excessively high calcination temperature, or taking out More complicated procedures such as grinding, so that not only cost and energy consumption can be saved, but the process is quite simple. Further, the apparatus for producing an adsorbent of the above embodiment of the present invention is simple, easy to obtain, and low in cost. Example 1 12.25 grams of carbonic acid was placed in the reactor. Thereafter, nitrogen gas is supplied from the gas supply device. The flow rate of nitrogen gas was 276 ml/min. The reactor pressure is atmospheric, and the calcination temperature and temperature rise time can be set by an example-integral-derivative (PID) controller. The calcination temperature was 85 Torr. 〇, the heating time is 13 W 29621twf.doc/n 201023969 30 minutes. When the reactor is heated to 20 (TC, the saturated steam supplied by the steam generation is introduced. The flow rate of the saturated steam is 525 liters/min. When the temperature of the reaction reaches 850 °C, the calcination time is maintained. After 3 minutes, the nitrogen gas was continuously supplied until the temperature of the reaction tube was lowered to 4 (10). The product was taken out, and then the product was analyzed by Scanning Electron Microscope (SEM). The adsorption and desorption test was carried out. The adsorption and desorption test was performed by a thermogravimetric analyzer (TGA) to analyze the weight change of calcium oxide formed by the adsorbent (having a pore size of 10 to 丨〇〇 nanometer). The reaction was carried out for 1 minute under nitrogen at 850 c. The adsorption was carried out for 5 minutes at 6% by volume (v/v) of carbon dioxide. 3 The results of SEM showed that the pore size of the calcium oxide in the adsorbent was ι〇 Nano ~100 nm. The specific surface area tester test 'its surface area up to 3 ^ square y grams. TGA analysis of the oxidative dance adsorbent of the embodiment of the present invention adsorption and desorption of carbon monoxide 1 〇 cycle weight change diagram Figure 2 shows the change in conversion rate The figure is shown in Figure 3. The results show that the adsorbent of the present invention can repeatedly adsorb and desorb carbon dioxide for at least one cycle, and the conversion rate can be at least 0 0.3, the adsorption amount is at least, and the gram dioxide hinders the A gram metal. Oxide. Comparative Example 1 j is similar to the method of Example i to make a wicking, but does not pass saturated steam, but directly passes nitrogen. The flow rate of nitrogen is 525 cc / min. # Figure 4 is a case of a car! And a comparison chart of the adsorption amount change of the adsorbent by the adsorption and desorption of the adsorbent prepared in the example i. The cycle of FIG. 4 shows 201023969

iW 29621twf.doc/n The sizing agent of Example 1 of the present invention can absorb the amount of carbon dioxide, reduce the rate of activity reduction, and greatly reduce the cost of capture. Example 2

12.25 grams of magnesium carbonate was placed in the reactor. Thereafter, nitrogen gas is supplied from the gas supply device. The flow rate of nitrogen is ΜNews/minute. The target temperature and temperature rise time of the reactor are set by the example_integration-derivative (PID) controller. The degree of calcination was 6 GG ° C 'the heating time was 3 σ minutes. When the reactor is warmed up to 20, the saturated steam supplied from the steam generating device is introduced. The flow rate of saturated helium gas was 525 ml/min. When the temperature of the reactor reached 60^#', the calcination time was maintained at 3G minutes. After the end of the calcination, the nitrogen gas was continuously introduced until the temperature of the reaction tube was lowered to 4 Torr (rc was taken out again. Thereafter, the obtained product was subjected to scanning electron microscopy (Sc_ing).

Electron Μ cut scope, SEM) slice analysis and perform suction and desorption test. The adsorption and desorption test is a thermogravimetric analyzer (TGA) to analyze the adsorbent (the pore size is 〇卜刚

The oxidation weight change of nano). Discharge in nitrogen for 1 minute. The adsorption is at 250. (: Contains 10% (v/v) of carbon dioxide for 11 minutes. . The results from SEM show that the pore size of calcium oxide in the adsorbent is 〇i nanometer ~1 〇〇 nanometer. Surface area tester test, its surface area The highest can be: square meters / gram. The adsorption amount is at least gram of oxidized metal before oxidation. Although the present invention has been implemented, the above is disclosed, and the present invention - any of the Reich Lai towels have the usual knowledge, in Doc/n 201023969 &gt; </ RTI> </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic diagram of an apparatus for preparing an adsorbent according to an embodiment of the present invention. FIG. 1 is a TGA analysis of the present invention--------------------------------------- Figure 3 is a graph showing the change in conversion rate of the oxygen-absorbing adsorbent of the present invention by the TGA analysis for 10 cycles of adsorption and desorption of carbon dioxide. Figure 4 is a comparison of Comparative Example 1 and the present invention. Huama adsorbent absorbs and desorbs carbon dioxide Comparison of changes in adsorption amount of the cycle. [Explanation of main component symbols] 10 Reactor 12 Temperature control device 14 Steam generation device 16 Gas supply device 18 Vapor separation device 20 Steam condensing device 22 Flowmeters 24a, 24b, 26a, 26b: Tube Road 100: Apparatus for preparing adsorbents 16

Claims (1)

29621twf.doc/n 201023969 X. Application for Patent Park: 1. A kind of adsorbent, including metal oxide, which has a plurality of pores with a diameter of 〇i nm~100 nm, and a specific surface area of 0.5~38.28 square Ruler / gram and attached at least G.25 grams of carbon dioxide / 1 gram of metal oxide. 2. The adsorbent of claim 1, wherein the adsorbent has a conversion of at least 0.3 ′ and can be repeatedly adsorbed and desorbed with carbon dioxide for 10 cycles. 3. The adsorbent of claim 1, wherein the metal oxide comprises an oxide of an alkaline earth element, an oxide of an alkali gold element, and a mixture thereof. 4. The adsorbent according to claim 1, further comprising a metal hydroxide, wherein the metal oxide is contained in an amount of 40% by weight to 80% by weight, and the metal hydroxide is present in an amount of 2% by weight. %~6〇% by weight. 5. The adsorbent of claim 4, wherein the metal hydroxide comprises a hydroxide of an alkaline earth element or a hydroxide of a gold group element or a mixture thereof. 6. The adsorbent according to claim 2, further comprising a metal niacin compound wherein the content of the metal oxide is from 75% by weight to 95% by weight, and the content of the metal carbonate compound is 5% by weight. 25 wt%. 7. The adsorbent according to claim 6, wherein the metal carbonate compound comprises a carbonate compound of an alkaline earth element, a carbonic acid compound of an alkali gold element or a mixture thereof. The adsorbent according to claim 1, wherein the adsorbent further comprises a metal hydroxide and a metal carbonate compound, wherein the metal oxygen 17 201023969, iW 29621twf.doc/n compound content is 30 weight %〜75重量%, the content of the metal hydroxide is 20% by weight to 5% by weight, and the content of the metal carbonate compound is 5% by weight to 25% by weight, and wherein the metal hydroxide comprises a soil-receiving element A hydroxide or a gold hydroxide of a gold group element or a mixture thereof. The metal carbonate compound includes a carbonic acid compound of a soil group element, a carbonic acid compound of an alkali gold group element, or a mixture thereof. 9. A method of regenerating a sorbent comprising: providing an adsorbent comprising a metal oxide, the adsorbent having adsorbed dioxin carbon; the adsorbent being in an environment containing saturated steam and at least one gas A calcination process is performed to regenerate the adsorbent; and carbon dioxide is adsorbed by the adsorbent that has been regenerated. 10. The method of the regeneration cycle of the adsorbent according to claim 9 wherein the metal oxide comprises an oxide of an alkaline earth element, an oxide of an alkali metal element or a mixture thereof. 11. The method of the regeneration cycle Φ of the adsorbent according to claim 9 wherein the volume ratio of the saturated steam to the gas (saturated water vapor/gas) is between 2 and 20. 12. The method of regenerating a sorbent according to claim 9, wherein the saturated water vapor has a flow rate of 165 to 1650 ml/min. 13. The method of the regeneration cycle of the adsorbent according to claim 9 wherein the flow rate of the gas is 8.25 to 825 ml/min. 14. The method of claim 9, wherein the gas comprises nitrogen, argon or a mixture thereof. K. A method of regenerating a sorbent according to claim 9 wherein the temperature of the calcination process is 25 〇u (9). 16. The method of regenerating the adsorbent according to claim 9 of the patent application, wherein the smelting cycle time is 1 G to 4 minutes. 17. The method of regenerating a sorbent according to claim 9, wherein the calcining process is carried out under normal pressure. 18. An apparatus for regenerating an adsorbent, comprising: a reactor for reacting an adsorbent having adsorbed carbon dioxide; a temperature control device coupled to the reactor for controlling a temperature of the reactor; a generating device coupled to the reactor for supplying a saturated water vapor to the reactor; a gas supply device coupled to the reactor for supplying at least one gas to the reactor; - Carbon oxide, helium, neon, and a vapor separation unit connected to the reactor for separating the saturated water vapor and the gas discharged from the reactor. 19. The apparatus for regenerating an adsorbent of claim 18, wherein the reactor comprises a fixed bed type, a fluidized bed type, a disturbed bed type or a high temperature resistant furnace. 20. The apparatus for regenerating a sorbent according to claim 18, wherein the vapor separation device comprises a vapor condensing device and a flow meter. 19