[0001]    This application is a divisional of U.S. non-provisional application Ser. No. 14/059,556 filed on Oct. 22, 2013 and also claims priority to provisional application Ser. No. 61/718807 filed Oct. 26, 2012 the contents of which are incorporated herein by reference. 
       BACKGROUND OF THE INVENTION 
       [0002]    This invention related to CO 2  capture and more particularly to a sorbent capable of capturing CO 2  at warm temperatures. 
         [0003]    There is a growing consensus that global warming is caused by anthropogenic CO 2  emission 1 . Among all sources, a coal-fired power plant represents the largest point source for CO 2  emission 2 . But at the same time, coal is the most inexpensive and most abundant fossil fuel 3 . Thus, in the near future, although renewable energy and nuclear energy will play increasing roles, coal will remain a major component of the energy portfolio, especially in developing counties 3 . Facing this dilemma, technologies are needed to utilize coal with higher energy efficiency and lower CO 2  emission. Currently, integrated gasification combined cycle with carbon capture and sequestration (IGCC with CCS) is one of the most promising candidates for achieving this goal 4 . IGCC has two important features compared with a traditional pulverized coal (PC) plant 5 . First, because of the combined cycle, IGCC can achieve higher energy efficiency. Second, the gas stream has higher pressure which facilitates the capture of sulfur, mercury, nitride oxide, particulate and CO 2 , making emission control less expensive. 
         [0004]    Currently, the state-of-the-art CO 2  capture process for IGCC is scrubbing the gas stream with physical or chemical solvents, such as MEA, Rectisol or Selexol. These solvent-based absorption processes need to operate at fairly low temperatures. Thus, the gas stream coming from a water gas shift reactor must be significantly cooled down, which leads to high energy loss and high capital costs both for the compressors used for cooling and for heat recuperation. A study carried out by DOE/NETL 5,6 , which assumed Selexol for carbon capture, indicated a reduction in net power output and a corresponding reduction in HHV thermal efficiency of 6%-9% as compared to a base case of IGCC with no carbon capture. It would be very desirable to reduce the parasitic energy load and operating costs associated with the traditional low-temperature CO 2  capture process. Prior studies have assessed high temperature CO 2  separation processes 7,8 , such as H 2 -permeable membranes 9,10 , CO 2 -premeable membrane 11 , and pressure swing adsorption (PSA) 12 , and identified opportunities to significantly improve the efficiency. A more recent study 13  in our group extended previous analyses to compare a variety of novel separation methods for IGCC with CCS, namely sorbents and membranes, on a unified basis. Our computational approach identified pressure swing adsorption operated at warm gas temperatures (200-300° C.) could be potentially more efficient compared with other approaches. However, no sorbent was yet reported to be applicable in this temperature range. 
         [0005]    Widely used in the oil and chemical industry, pressure swing adsorption 20  (PSA) of gases onto solid sorbents provides some key advantages, such as low energy requirements, low costs, and ease of applicability. In spite of these advantages, there have only been a few studies related to regenerable sorbents of CO 2  at 200-300° C. in the literature. To be applicable to a PSA process in the desired temperature range, the sorbent needs to maintain a regenerable sorbent capacity, fast kinetics, and low heat of adsorption. The commercially available sorbents such as activated carbon, zeolites, and alumina lose their adsorption properties at temperatures higher than 150° C., Super activated carbon 21  can maintain sufficient capacity at temperatures as high as 220° C., but the CO 2 /N 2  selectivity is low. Basic zeolites 22,23  obtained by doping with electropositive ions were also tested for this purpose, hut showed poor performance in the presence of other polar gases such as SO 2  and steam. 
         [0006]    Some inorganic materials have also been proposed in the literature for carbon capture at an elevated temperature, such as calcium oxide 24,25 , lithium zirconate 26 , lithium silicate 27,28 , sodium-based sorbent 29 , hydrotalcite-like compounds (HTls) 30,31  and double salt sorbent 32 . Calcium oxide demonstrated high capacity even, at 700° C., but suffered from poor regenerability, slow kinetics and an extremely large heat requirement. Lithium-based materials can capture CO 2  in the 450-550° C. range, but suffer from slow sorption kinetics. Sodium-based materials showed good adsorption in the 200-400° C. range, but the materials can only be regenerated at 700° C., and so are not suitable for pressure swing adsorption. Double salt sorbent shows extremely high capacity at high temperature, but it is very hard to produce reproducible samples 33 . Recently, DOE/NETL reported a magnesium hydroxide based sorbent 19 , which has a large capacity in the 200-300° C. range, and can be regenerated at 375° C. But the re-generation via thermal treatment is still not desirable for our purpose. In addition, the breakthrough curve of this sorbent indicates slow sorption kinetics which could arise from the very low surface area of the sorbent. Among such inorganic materials, HTls stand out as the most promising candidate for warm CO 2  capture, and they have been widely studied for sorption-enhanced water gas shifter reaction 34,35 . Hydrotalcite-like compounds consist of positively-charged brucite (MgOH)-like layers balanced by hydrated anions. The most common type is Mg—Al—CO 3 , in which stacked layers of magnesium hydroxide [Mg(OH) 2 ] in which some of the divalent cations (Mg 2+ ) are substituted by trivalent cations (Al 3+ ) at the centers of octahedral sites of the hydroxide sheets. HTls are often promoted with K 2 CO 3  to improve their performance in the presence of high pressure steam. These two classes of materials after calcination have been widely studied for CO 2  capture at high temperatures (350-500° C.). 
         [0007]    This patent application has as an object to develop a new sorbent for CO 2  with good regenerability, fast kinetics and low heat of adsorption that can be applied in a PSA process in a warm temperature range. The material prepared through incipient wetness impregnation has a large surface area and pore size which facilitates the rapid adsorption of CO 2 . Through the detailed study of sorbent capacity, multi-cycle regenerability, sorption rate and comparisons with HTls, we demonstrate here that the sorbent disclosed herein is a candidate for warm CO 2  capture by the PSA process. 
       SUMMARY OF THE INVENTION 
       [0008]    According to the invention, a sorbent for reversible warm CO 2  capture includes a high surface area support material impregnated with MgO, wherein the MgO constitutes at least 5% by weight of the sorbent. A preferred high surface area support material is activated carbon. In a preferred embodiment, MgO constitutes approximately 15% by weight. MgO in the range of 5-15% is suitable for uses in the invention. It is preferred that the sorbent material disclosed herein be made using an incipient wetness impregnation method. In a preferred embodiment, a magnesium precursor is a soluble magnesium salt such as magnesium nitrate. 
         [0009]    The sorbent disclosed herein has good regenerability, fast kinetics, and low heat of adsorption that can be applied in a pressure swing adsorption process at a warm temperature range. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWING 
         [0010]      FIG. 1  is a thermogravimetric diagram of the formation of the sorbent disclosed herein from a precursor material. 
           [0011]      FIG. 2  is a graph showing the pore size distribution of an embodiment of the support and sorbent disclosed herein. 
           [0012]      FIG. 3  is a graph of quantity adsorbed as a function of relative pressure for N 2  sorption-desorption tests. 
           [0013]      FIG. 4  is a schematic diagram of a high pressure microbalance system. 
           [0014]      FIG. 5  is a graph of capacity versus pressure showing reversible adsorption isotherms at various temperatures. 
           [0015]      FIG. 6  is a graph of differential heat of adsorption against capacity showing that heat of adsorption has a weak dependence on loading. 
           [0016]      FIG. 7  is a graph of capacity against cycle number for sorbent at 200° C. 
           [0017]      FIG. 8  is a thermogravimetric diagram of the sorbent disclosed herein when exposed to one atmosphere CO 2  at different temperatures. 
           [0018]      FIG. 9  is a graph of sorption rate against time at different temperatures when exposed to one atmosphere CO 2 . 
           [0019]      FIG. 10  is a graph of capacity against cycle number providing cyclic working capacity comparisons of the sorbent disclosed herein versus HTLs. 
           [0020]      FIG. 11  is a graph of normalized capacity against time showing sorption rate comparisons. 
       
    
    
     DESCRIPTION OF THE PREFERRED EMBODIMENT 
       [0021]    The sorbent material of the invention was synthesized using the incipient wetness impregnation method, which has been widely adopted for preparing heterogeneous catalysts. Those of skill in the art will recognize that other methods for depositing MgO on the support may be used including co-precipitation, sol gel method, electrolytic processing, and chemical vapor deposition. An MgO/carbon sorbent can be made in one step using MgCl 2  as a chemical activation reagent for activated carbon production. This process makes the production cost very low, which is a key factor when choosing a sorbent. To achieve the best performance, different magnesium precursors (nitrate, citrate, acetate, oxalate) were tested and compared. Nitrate was finally chosen as the precursor. Several preparation conditions, such as precursor concentration, support materials, calcination temperature and time were also studied to determine the optimal preparation procedure. The finalized impregnation procedure is as follows: 3.8 M solution of MgCNO 3 ) 2  (from Sigma Aldrich) was added dropwise to preheated activated carbon (DARCO®, from Sigma Aldrich), to reach the desired MgO loading (15% by weight in a preferred embodiment). The as-prepared material was first dried for 12 h in open air, and was further dried in an oven at 100° C. for another 12 h. The material was finally calcined in a muffle furnace at 500° C. for 3 h under pure nitrogen. 
         [0022]    It is recognized that other high surface area supports beyond activated carbon may be used in the present invention including Metal-Organic Frameworks (MOF), zeolites, activated alumina and mesoporous silica. Some of these support materials might require modification of the impregnation method such as, for example, to use a nonaqueous solvent rather than water. 
         [0023]    The formation of the sorbent from the supported magnesium precursor was characterized by thermogravimetric analysis (TGA) in a thermogravimetric analyzer (Q500 TGA, TA Instruments). The typical thermogravimetric profile of the material is shown in  FIG. 1 . The material showed three decomposition steps leading to the corresponding sorbent. A first region showed water loss with a broad peak from 350K-450K. Most of the loosely held water in the precursor was lost before the materials reached 463 K. The second region (450K-700 K) showed an intense endothermic peak which corresponds to decomposition of magnesium nitrate to magnesium oxide. The third region (700K-900K) has no observable peak, and the small weight change might arise from the weight loss of the carbon support. A temperature of 750K was finally chosen as the calcination temperature, as this would ensure the minimum sintering and complete decomposition of magnesium nitrate. 
         [0024]    The surface area and pore size distribution of the sorbent were determined by N 2  adsorption-desorption isotherms at 77 K on a Micromeritics ASAP 2020 instrument. The surface areas and average pore diameters (Dp) were calculated using the Brunauer-Emmett-Teller (BET) method. The pore size distributions and pore volumes (Vp), between 170 and 300 nm, were determined from the desorption branch using the Barrett-Joyner-Halenda (BJH) method. See  FIG. 2 . 
         [0025]    As shown in  FIG. 3 , both of the materials show characteristic hysteresis loops of the type IV isotherm 14 , which is associated with capillary condensation taking place in mesopores. This type of isotherm is very common in mesoporous industrial adsorbents. 
         [0026]    Analysis of the hysteresis loops indicates that samples synthesized by incipient wetness impregnation did not exhibit any limiting adsorption at high relative pressure, which is characteristic of type H3 hysteresis loops, corresponding to aggregates of plate-like particles giving rise to slit-shaped pores 14 . In general, the porous structure patterns measured by BET were maintained after the impregnation and the subsequent thermal treatment despite the observed decreases in surface area. 
         [0027]    The morphological properties of the support and sorbent are summarized in Table 1. As expected, heat treatment of the samples reduced their specific surface areas and mesopores volumes. But the average pore diameter does not change significantly. These values ensure that the pore size is not limiting with respect to the subsequent CO 2  adsorption studies. The total volume was contributed mostly from mesoporosity volume. 
         [0000]    
       
         
               
             
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Summary of morphological data for the support and sorbet 
               
             
          
           
               
                   
                 BET surface area 
                 Total pore volume  
                 V_2 nm-300 nm 
                 Dp  
               
               
                   
                 (m2/g) 
                 (cm3/g) 
                 (cm3/g) 
                 (nm) 
               
               
                   
               
               
                 Support 
                 978 
                 0.82 
                 0.55 
                 6.84 
               
               
                 Sorhent 
                 532 
                 0.48 
                 0.34 
                 6.93 
               
               
                   
               
             
          
         
       
     
         [0028]    The measurements of sorption capacity and cyclic stability of the sorbent were performed in a high pressure microbalance shown in  FIG. 4  (D110, from THASS company, Germany) and a TGA analyzer (Q 500 TGA, TA Instruments). A buoyancy correction has been considered. 
         [0029]    The combined isotherm containing reversible and irreversible components was first determined, and the sample was then evacuated to remove only the reversibly adsorbed CO 2 . The adsorption isotherm was then measured again, yielding the reversible adsorption only. The irreversible adsorption was determined by the difference between the total isotherms and reversible isotherm at different pressure points. The capacity for reversible and irreversible adsorption at different temperatures are summarized in Table 2. 
         [0000]    
       
         
               
             
               
               
               
               
               
             
               
               
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 Capacity at different temperature and pressure (mmol CO 2 /g Sorbent) 
               
             
          
           
               
                 Pressure  
                 T = 180° C. 
                 T = 200° C.  
                 T = 220° C. 
                 T = 240° C. 
               
             
          
           
               
                 atm 
                 Reversible  
                 Irreversible  
                 Reversible  
                 Irreversible  
                 Reversible  
                 Irreversible  
                 Reversible  
                 Irreversible 
               
               
                   
               
             
          
           
               
                 3 
                 0.6416 
                 0.2386 
                 0.5595 
                 0.2064 
                 0.4775 
                 0.2235 
                 0.4438 
                 0.1648 
               
               
                 4 
                 0.7803 
                 0.2481 
                 0.7004 
                 0.2159 
                 0.5909 
                 0.2159 
                 0.5615 
                 0.1761 
               
               
                 5 
                 0.9002 
                 0.2689 
                 0.8097 
                 0.2386 
                 0.6876 
                 0.2311 
                 0.6518 
                 0.1913 
               
               
                 6 
                 0.9969 
                 0.3011 
                 0.9211 
                 0.2424 
                 0.7780 
                 0.2462 
                 0.7296 
                 0.2121 
               
               
                 7 
                 1.1189 
                 0.3011 
                 1.0347 
                 0.2557 
                 0.8769 
                 0.2576 
                 0.8306 
                 0.2178 
               
               
                 8 
                 1.2410 
                 0.3068 
                 1.1442 
                 0.2633 
                 0.9779 
                 0.2765 
                 0.9232 
                 0.2292 
               
               
                 9 
                 1.3273 
                 0.3106 
                 1.2200 
                 0.2803 
                 1.0579 
                 0.2803 
                 0.9927 
                 0.2311 
               
               
                 10 
                 1.4200 
                 0.3220 
                 1.3106 
                 0.2898 
                 1.1422 
                 0.2917 
                 1.0707 
                 0.2462 
               
               
                 11 
                 1.4959 
                 0.3371 
                 1.3864 
                 0.3011 
                 1.1992 
                 0.3049 
                 1.1318 
                 0.2443 
               
               
                 12 
                 1.5697 
                 0.3428 
                 1.4645 
                 0.3106 
                 1.2835 
                 0.2992 
                 1.2141 
                 0.2443 
               
               
                 13 
                 1.6436 
                 0.3485 
                 1.5342 
                 0.3106 
                 1.3490 
                 0.3049 
                 1.2816 
                 0.2557 
               
               
                 14 
                 1.7028 
                 0.3655 
                 1.6081 
                 0.3163 
                 1.4082 
                 0.3144 
                 1.3555 
                 0.2424 
               
               
                 15 
                 1.7788 
                 0.3598 
                 1.6652 
                 0.3295 
                 1.4800 
                 0.3125 
                 1.4232 
                 0.2405 
               
               
                 16 
                 1.8865 
                 0.3580 
                 1.7813 
                 0.3163 
                 1.5793 
                 0.3163 
                 1.5056 
                 0.2462 
               
               
                   
               
             
          
         
       
     
         [0030]    Concerning the effect of temperature, it was observed that the capacity of the adsorption decreases as the temperature increases, because high temperature shifts the adsorption reaction equilibrium. The reversible adsorption capacity shows a strong dependence on the partial pressure of CO 2 , and the trend can be fitted to a Langmuir model with good precision. The irreversible adsorption capacity reaches a relatively high value even at a low pressure, and the pressure increase does not significantly increase the irreversible adsorption capacity. The irreversible adsorption sites get saturated even at lower pressure, suggesting the irreversible adsorption arises from a strong chemical reaction, which is sharply different from the reaction mode contributing to the reversible adsorption. 
         [0031]    For a practical pressure swing absorption sorbent, we care only about the reversible adsorption, because only reversible components would contribute in a real application. A reversible adsorption isotherm at four different temperatures was measured in the high pressure microbalance, and the measurement has been corrected by considering buoyancy effects. 
         [0000]    
       
         
           
             
               
                 
                   
                     n 
                     i 
                     0 
                   
                   = 
                   
                     
                       a 
                        
                       
                           
                       
                        
                       
                         exp 
                          
                         
                           ( 
                           
                             b 
                             / 
                             T 
                           
                           ) 
                         
                       
                        
                       P 
                     
                     
                       1 
                       + 
                       
                         c 
                          
                         
                             
                         
                          
                         
                           exp 
                            
                           
                             ( 
                             
                               d 
                               / 
                               T 
                             
                             ) 
                           
                         
                          
                         P 
                       
                     
                   
                 
               
               
                 
                   Equation 
                    
                   
                       
                   
                    
                   1 
                 
               
             
           
         
       
     
         [0032]    A temperature-dependent Langmuir model (Equation 1) was adopted to fit the isotherm data. As shown in  FIG. 5 , the model captures the shape and temperature-dependent behavior. 
         [0033]    The heat of adsorption is rigorously derived in the literature 15-17  as shown in Equation 2, where n i   0  is the capacity. Once a temperature-dependent equilibrium isotherm is established, the heat of adsorption can be theoretically derived from an isotherm model based on Equation 3. The heat of adsorption for this sorbent is shown in  FIG. 6 , which is consistent with reported data 18 . The value is very close to the enthalpy of reaction between magnesium hydroxide and CO 2   19  which is consistent with the analysis concerning the correlation between reaction mode and reversibility 18 . 
         [0000]    
       
         
           
             
               
                 
                   
                     q 
                     i 
                     0 
                   
                   = 
                   
                     
                       
                         RT 
                         2 
                       
                        
                       
                         [ 
                         
                           
                             
                               ∂ 
                               ln 
                             
                              
                             
                                 
                             
                              
                             P 
                           
                           
                             ∂ 
                             T 
                           
                         
                         ] 
                       
                     
                     
                       n 
                       i 
                       0 
                     
                   
                 
               
               
                 
                   Equation 
                    
                   
                       
                   
                    
                   2 
                 
               
             
             
               
                 
                   
                     q 
                     i 
                     0 
                   
                   = 
                   
                     
                       - 
                       
                         
                           R 
                           ( 
                           
                             
                               ∂ 
                               
                                 n 
                                 i 
                                 0 
                               
                             
                             
                               ∂ 
                               
                                 ( 
                                 
                                   1 
                                   / 
                                   T 
                                 
                                 ) 
                               
                             
                           
                           ) 
                         
                         P 
                       
                     
                     / 
                     
                       
                         ( 
                         
                           
                             ∂ 
                             
                               n 
                               i 
                               0 
                             
                           
                           
                             
                               ∂ 
                               ln 
                             
                              
                             
                                 
                             
                              
                             P 
                           
                         
                         ) 
                       
                       T 
                     
                   
                 
               
               
                 
                   Equation 
                    
                   
                       
                   
                    
                   3 
                 
               
             
           
         
       
     
         [0034]    As stressed above, to be applicable in the pressure swing adsorption process, regenerability is an important property. To study the adsorption reversibility, an 84-cycle test was performed in a high pressure microbalance. The temperature was maintained at 200° C. The sorption step was at 13 atm and the desorption was at 1 atm. 
         [0035]    It was observed ( FIG. 7 ) that the capacity at the 1st cycle is large, which is attributed to the combination of reversible and irreversible adsorption. The capacity decreases dramatically after the first cycle. Roughly 30% of the capacity cannot be regenerated using pressure change only as discussed above. The sorbent can only be completely regenerated at high temperature (723K). 
         [0036]    After the first cycle, the sorbent can maintain a capacity of roughly 1.4 mmol/g. According to the study 18 , the irreversibility arises from the formation of unidentate carbonates. The decrease of surface area could also contribute to the capacity reduction. 
         [0037]    The sorbent capacity is lower than that of the commonly reported activated carbon and zeolites. But note that those sorbents are working at much lower temperature, and at low temperature, multilayer adsorption contributes to the high capacity. These multilayer sorbents do not work in our desired temperature range. On the other hand, calcium oxide and lithium based materials have a very large capacity at high temperature, but in those cases, the sorption is based on bulk reaction. The drawback of that sorption mode is the extremely slow kinetics associated with bulk reaction and species diffusion in a solid. The novel sorbent disclosed herein apparently captures CO 2  based on purely a surface reaction. One can treat it as a pseudo-single layer adsorption. Considering the surface area of the sorbent, the capacity data is reasonable. 
         [0038]    Adsorption rate is another important criterion in selecting a sorbent. To be applicable for pressure swing adsorption, the sorption rate needs to be fast to reduce the overall cycle time.  FIG. 8  indicates that the weight increases rapidly in the first 2 minutes. The differential weight change indicates significant sorption in less than 1 min. Concerning the effect of temperature, we note that the sorption capacity decreases as temperature increases. But the sorption rate is slightly faster at higher temperature which is typical behavior for a chemical reaction.  FIG. 9  shows sorption rate at different temperatures. 
         [0039]    Compared with the sorption rate of commercially-available low temperature PSA sorbents, like activated carbon and zeolites, the sorption rate of our new sorbent is slower. That is because these sorbents capture CO 2  purely based on weak physical interaction. In those cases, the limiting step is mass transfer. However, in our case, the sorption mechanism is based on a surface chemical reaction. It is reasonable to observe a relatively slower sorption rate. 
         [0040]    It should be noted that it is a common problem for high temperature sorbents to have slow sorption kinetics, because the sorption is based on chemical reaction, surface or bulk, rather than a weak physical interaction with lower energy barrier. Sorbents like calcium oxide and lithium-based materials capture CO 2  based on bulk reaction. The sorption kinetics can only be improved by increasing the working temperature or by doping which improves the bulk phase mass transfer. But the drawback for this sorption mode is bulk reaction normally leads to a change of crystal structure of sorbent. The sorbent needs a higher temperature to be regenerated, which always results in a decreasing working capacity. The material disclosed here captures CO 2  based on a surface reaction. What we want to stress here is, a sorbent with high surface area, high surface biding site density which captures CO 2  based on a weakly-exothermic surface reaction would reasonably be the better candidate for the PSA process in our temperature of interest (200-300° C.). 
         [0041]    To compare our sorbent with the well-studied HTls discussed above, a reversibility and kinetics comparison was performed in a TGA at 200° C. and 1 atm CO 2 . As shown in  FIG. 10 , all materials show a large capacity in the first cycle, but the capacity of HTls dramatically decrease after the first cycle, indicating most of the surface reaction is irreversible at this temperature. The capacity for HTls keeps decreasing in the 10-cycle tests, while the MgO/C sorbent maintains a stable and larger reversible capacity. The sorption rate for these three samples was also compared. As shown in  FIG. 11 , the MgO/C has a much faster sorption rate compared with HTls at 200° C. These two comparisons indicate MgO/C is a better candidate for warm CO 2  capture in the temperature range of interest. MgO/C provides advantages over HTls in both regenerable capacity and sorption rate. 
         [0042]    The superscript numbers refer to the list of references included herewith, the contents of all of which are incorporated herein by reference. 
         [0043]    The sorbent disclosed herein has been rigorously analyzed in “Analysis of adsorbent-based warm CO2 capture technology for integrated Gasification Combined Cycle (IGCC) power plants,” Ind. Eng. Chem. Res., the contents of which are incorporated by reference. 
         [0044]    It is also recognized that a sorbent within the scope of this invention may begin with a magnesium compound other than MgO such as Mg(OH) 2  or MgCO 3  that will convert to MgO during operation thus failing within the scope of the appended claims. 
         [0045]    It is recognized that modifications and variations of the invention will be apparent to those of ordinary skill in the art, and it is intended that all such modifications and variations be included within the scope of the appended claims. 
       REFERENCES 
       [0000]    
       
         (1) Solomon, S.; Qin, D.; Manning, M.; Marquis, M.; Averyt, K.; Tignor, M. M. B.; Miller, H. L.; Chen, Z.  Climate Change  2007 —The Physical Science Basis ; Cambridge University Press, 2007; pp. 665-670. 
         (2) Katzer, J.; Ansolahehere, S.; Beer, J.; Deutch, J.; Ellerman, A. D.; Friedmann, S. J.; Herzog, H.; Jacoby, H. D.; Joskow, P. L.; McRae, G.; Lester, R.; Moniz, E. J.; Steinfeld, E.  The Future of Coal ; Massachusetts Institute of Technology, 2007. 
         (3) DOE/EIA  International Energy Outlook  2001; 2011. 
         (4) Frey, H. C.; Zhu, Y. Improved system integration for integrated gasification combined cycle (IGCC) systems.  Environmental science  &amp;  technology  2006, 40, 1693-9. 
         (5) DOE/NETL  Fossil Energy Power Plant Desk Reference;  2007. 
         (6) DOE/NETL  Cost and Performance Baseline for Fossil Energy Plants;  2007; Vol. 1. 
         (7) DOE/NETL  Current and Future Technologies for Gasification - Based Power Generation;  2010; Vol. 2. 
         (8) Schlatter, J.; Turk, B. Desulfurization Process versus Traditional Scrubbers for a Warm Syngas Cleanup Technologies, In  Gasification Technologies Conference;  2007. 
         (9) Amelio, M.; Morrone, P.; Gallucci, F.; Basile, A. Integrated gasification gas combined cycle plant with membrane reactors: Technological and economical analysis.  Energy Conversion and Management  2007, 48, 2680-2693. 
         (10) P., C.; Kreutz, T.; Lozza, G. CO2 Sequestration From IGCC Power Plants by Means of Metallic Membranes. 2007, 129, 123-134. 
         (11) Grainger, D.; Hägg, M.-B. Techno-economic evaluation of a PVAm CO2-selective membrane in an IGCC power plant with CO2 capture.  Fuel  2008, 87, 14-24. 
         (12) Ito, S.; Makino, H. Carbon Dioxide Separation from Coal Gas by Physical Adsorption at Warm Temperature. In  Greenhouse Gas Control Technologies;  1998; pp. 131-136. 
         (13) Cooling, D. J.; Prakash, K.; Green, W. H. Analysis of Membrane and Adsorbent Processes for Warm Syngas Cleanup in Integrated Gasification Combined-Cycle Power with CO2 Capture and Sequestration.  Ind. Eng. Chem. Re .  2011, 50, 11313-11336. 
         (14) IUPAC REPORTING PHYSISORPTION DATA FOR GAS/SOLID SYSTEMS with Special Reference to the Determination of Surface Area and Porosity (Recommendations 1984),  Pure  &amp;  Appt. Chem.  1985, 57, 603-619. 
         (15) Sircar, S. Isosteric heats of multicomponent gas adsorption on heterogeneous adsorbents.  Langmuir  1991, 7, 3065-3069. 
         (16) Sircar, S.; Mohr, R.; Ristic, C.; Rao, M. B. Isosteric Heat of Adsorption: Theory and Experiment.  J. Phys. Chem. B  1999, 103, 6539-6546. 
         (17) Sircar, S. Excess properties and thermodynamics of multicomponent gas adsorption.  Journal of the Chemical Society, Faraday Transactions l  1985, 81, 1527-1540. 
         (18) Leon, M.; Diaz, E.; Bennici, S.; Vega, A.; Ordonez, S.; Auroux, A. Adsorption of CO2 on Hydrotalcite-Derived Mixed Oxides: Sorption Mechanisms and Consequences for Adsorption Irreversibility.  Ind. Eng. Chem. Res.  2010, 49, 3663-3671. 
         (19) Siriwardane, R. V.; Stevens, R. W. Novel Regenerable Magnesium Hydroxide Sorbents for CO2 Capture at Warm Gas Temperatures,  Ind. Eng. Chem. Res.  2009, 48, 2135-2141. 
         (20) Ruthven, D. M.; Farooq, S.; Knaebel, K. S.  Pressure Swing Adsorption ; VCH Publisher, 1994; pp. 221-264. 
         (21) Kyaw, K.; Shibata, T.; Watanabe, P.; Matsuda, H.; Hasatani, M. Applicability of zeolite for CO2 storage in a CaO—CO2 high temperature energy storage system, Energy Conversion and Management 1997, 38, 1025-1033. 
         (22) Díaz, E.; Muñoz, E.; Vega, A.; Ordóñez, S. Enhancement of the CO(2) retention capacity of X zeolites by Na- and Cs-treatments.  Chemosphere  2008, 70, 1375-82. 
         (23) Díaz, E.; Muñoz, E.; Vega, A.; Ordóñez, S. Enhancement of the CO 2 Retention Capacity of Y Zeolites by Na and Cs Treatments: Effect of Adsorption Temperature and Water Treatment.  Ind. Eng. Chem. Res.  2008, 47, 412-418. 
         (24) Beruto, D.; Botter, R.; Searcy, A. W. Thermodynamics and Kinetics of Carbon Dioxide Chemisorption on Calcium Oxide,  J. Phys. Chem  1984, 88, 4052-4055. 
         (25) Filitz, R.; Kierzkowska, A. M.; Broda, M.; Müller, C. R. Highly efficient CO2 sorbents: development of synthetic, calcium-rich dolomites.  Environmental science  &amp;  technology  2012, 46, 559-565. 
         (26) Nakagawat, K.; Ohashi, T. A Novel Method of CO2 Capture from High Temperature Gases.  J. Electrochem. Soc.  1998, 145, 1344-1346. 
         (27) Bretado, M. E.; Guzmán Velderrain, V.; Lardizábal Gutiérrez, D.; Collins-Martínez, V.; Ortiz, A. L. A new synthesis route to Li4SiO4 as CO2 catalytic/sorbent.  Catalysis Today  2005, 107-108, 863-867. 
         (28) Gauer, C.; Heschel, W. Doped lithium orthosilicate for absorption of carbon dioxide.  Journal of Materials Science  2006, 41, 2405-2409. 
         (29) Siriwardane, R. V.; Robinson, C.; Shen, M.; Simonyi, T. Novel Regenerable Sodium-Based Sorbents for CO 2 Capture at Warm Gas Temperatures.  Energy  &amp;  Fuels  2007, 21, 2088-2097. 
         (30) Ding, Y.; Alpay, E. Equilibria and kinetics of CO2 adsorption on hydrotalcite adsorbent.  Chemical Engineering Science  2000, 55, 3461-3474. 
         (31) Yong, Z.; Rodrigues, A. E. Hydrotalcite-like compounds as adsorbents for carbon dioxide.  Energy Conversion and Management  2002, 43, 1865-1876. 
         (32) Mayorga, S. G.; Weigel, S. J.; Gaffney, T. R.; Brzozowski, J. R.  Carbon Dioxide Adsorbents Containing Magnesium Oxide Suitable for Use at Hight Temperature ; U.S. Pat. No. 6,280,503 B1. 
         (33) Singh, R.; Ram Reddy, M. K.; Wilson, S.; Joshi, K.; Diniz da Costa, J. C.; Webley, P. High temperature materials for CO2 capture.  Energy Procedia  2009, 1, 623-630. 
         (34) van Selow, E. R.; Cobden, P. D.; Verbraeken, P. a.; Hufton, J. R.; van den Brink, R. W. Carbon Capture by Sorption-Enhanced Water—Gas Shift Reaction Process using Hydrotalcite-Based Material.  Industrial  &amp;  Engineering Chemistry Research  2009, 45, 4184-4193. 
         (35) van Selow, E. R.; Cobden, P. D.; Wright, a. D.; van den Brink, R. W.; Jansen, D. Improved sorbent for the sorption-enhanced water-gas shift process.  Energy Procedia  2011, 4, 1090-1095. 
         (36) Larson, E. D.; Jin, H.; Celik, F. E. Large-scale gasification-based coproduction of fuels and electricity from switchgrass.  Biofuels, Bioproducts and Biorefining  2009, 5, 174-194. 
         (37) Chiesa, P.; Consonni, S.; Kreutz, T. Co-production of hydrogen, electricity and CO from coal with commercially ready technology. Part A: Performance and emissions.  International Journal of Hydrogen Energy  2005, 30, 747-767. 
         (38) Kreutz, T.; Williams, R.; Consonni, S.; Chiesa, P. Co-production of hydrogen, electricity and CO from coal with commercially ready technology. Part B: Economic analysis.  International Journal of Hydrogen Energy  2005, 30, 769-784.
Sorbent for reversible warm CO 2 capture. The sorbent includes activated carbon impregnated with magnesium oxide, wherein the magnesium oxide constitutes at least 5% by weight of the sorbent.