# Patent

## Title
Metal-organic materials (MOMS) for CO2 adsorption and methods of using MOMS

## Abstract

Embodiments of the present disclosure provide for hydrophobic multi-component metal-organic materials (MOMs) (also referred to as “hydrophobic MOM”), systems that exhibit permanent porosity and using hydrophobic MOMs to separate components in a gas, methods of separating CO2 from a gas, and the like.

## Background
CROSS-REFERENCE TO RELATED APPLICATION
This application is a continuation of and claims priority to application Ser. No. 13/800,690, entitled “Metal-Organic Materials (MOMS) for CO2 Adsorption and Methods of Using MOMS”, filed Mar. 13, 2013, which claims priority to U.S. provisional application entitled “Metal Organic Composition, for Carbon Dioxide Separation and Capture,” having Ser. No. 61/682,017, filed on Aug. 10, 2012, which is entirely incorporated herein by reference. The application having Ser. No. 13/800,690 also claims priority to U.S. provisional application entitled “Metal Organic Composition, for Carbon Dioxide Separation and Capture,” having Ser. No. 61/723,533, filed on Nov. 7, 2012, which is entirely incorporated herein by reference.


BACKGROUND
Metal-organic framework (MOF) materials that exhibit permanent porosity have received extensive interest due to their potential applications for gas storage or capture. However, many of the currently used MOFs have limitations, in particular, use in humid conditions, and thus, other types of MOFs having desired characteristics are needed to be used in certain applications.
SUMMARY
Embodiments of the present disclosure provide for hydrophobic multi-component metal-organic materials (MOMs) (also referred to as “hydrophobic MOM”) systems that exhibit permanent porosity and using hydrophobic MOMs to separate components in a gas, methods of separating CO2 from a gas, and the like.
An embodiment of the method of capturing CO2 in a gas, among others, includes: exposing the gas to a hydrophobic multicomponent metal-organic material (MOM) (e.g., have a primitive cubic topology), wherein the gas includes CO2 and water vapor, wherein the MOM has a greater relative affinity for CO2 over the water vapor; and capturing the CO2 in the MOM through adsorption.
An embodiment of the system for capturing CO2 in a gas mixture, among others, includes: a first structure including a hydrophobic multicomponent metal-organic material (MOM) having a primitive cubic topology, wherein the gas includes CO2 and water vapor, wherein the MOM has a greater relative affinity for CO2 over the water vapor; and a second structure for introducing the gas to the first structure, wherein CO2 is removed from the gas after the exposure to the hydrophobic MOM to form a modified gas, wherein the second structure flows the modified gas away from the first structure.
An embodiment of the method of separating components in a gas mixture, among others, includes: exposing a gas including a first component and a second component to a hydrophobic multicomponent metal-organic material (MOM) having a primitive cubic topology, wherein the MOM has a greater relative affinity for the first component over a second component; and capturing the first component in the MOM.
An embodiment of the system for separating components in a gas mixture, among others, includes: a first structure including a hydrophobic multicomponent metal-organic material (MOM) having a primitive cubic topology, wherein the gas includes a first component and a second component, wherein the MOM has a greater relative affinity for the first component over the second component; and a second structure for introducing the gas to the first structure, wherein first component is removed from the gas after the exposure to the hydrophobic MOM to form a modified gas, wherein the second structure flows the modified gas away from the first structure.



BRIEF DESCRIPTION OF THE DRAWINGS
Many aspects of the disclosed devices and methods can be better understood with reference to the following drawings. The components in the drawings are not necessarily to scale, emphasis instead being placed upon clearly illustrating the relevant principles. Moreover, in the drawings, like reference numerals designate corresponding parts throughout the several views.
FIG. 1: The variable pore size channel structures of SIFSIX-2-Cu, SIFSIX-2-Cu-i and SIFSIX-3-Zn.a, SIFSIX-2-Cu; pore size 13.05 Å, BET apparent surface area (N2 adsorption) 3,140 m2 g−1. b, SIFSIX-2-Cu-i; pore size 5.15 Å, BET apparent surface area (N2 adsorption) 735 m2 g−1. c, SIFSIX-3-Zn; pore size 3.84 Å, apparent surface area (determined from CO2 adsorption isotherm) 250 m2 g−1. Color code: C (grey), N (blue (dark gray)), Si (yellow (medium gray)), F (light blue (light gray)), H (white). All guest molecules are omitted for clarity. Note that the green (dark grey) net represents the interpenetrated net in SIFSIX-2-Cu-i. The nitrogen-containing linker present in SIFSIX-2-Cu and SIFSIX-2-Cu-i is 4,4′-dipyridylacetylene (dpa) whereas that in SIFSIX-3-Zn is pyrazine (pyr). The lower portion is a schematic of a basic structure of the MOM.
FIG. 2: (a) Variable temperature CO2 sorption isotherms for SIFSIX-2-Cu-i and (b) SIFSIX-3-Zn; (c) Qst of CO2 adsorption on SIFSIX-2-Cu-i and SIFSIX-3-Zn in the low pressure region; (d) The modeled structure of a 3×3 box of unit cells of SIFSIX-3-Zn reveals close interactions between the electropositive carbon atoms of CO2 molecules and fluoride atoms of SIFSIX anions; (e) Column breakthrough experiment for CO2/N2:10/90 gas mixture (298 K, 1 bar) carried out on SIFSIX-2-Cu-i and SIFSIX-3-Zn; (f) Column breakthrough experiment for CO2/CH4:50/50 gas mixture (298 K, 1 bar) carried out on SIFSIX-2-Cu-i and SIFSIX-3-Zn.
FIG. 3: (a) IAST CO2 adsorption selectivity for a CO2/CH4 mixture on SIFSIX-2-Cu-i and SIFSIX-3-Zn vs. Mg-dobdc and 13X zeolite at 298K. Experimental data using gravimetric-densimetric-gas analysis is provided for comparison; (b) IAST CO2/CH4:50:50 adsorption isotherm prediction compared to experimental pure CO2, CH4 and CO2/CH4:50:50 gas mixture adsorption isotherms collected for SIFSIX-3-Zn at 298 K; (c) CO2 adsorption selectivity of SIFSIX-2-Cu-i, SIFSIX-3-Zn and 13X zeolite for CO2/N2:10:90 as calculated using IAST at 298 K; (d) IAST CO2/N2:10:90 adsorption isotherm predictions compared to experimental pure CO2, N2 and CO2/N2:10:90 gas mixture adsorption isotherms collected for SIFSIX-3-Zn at 298 K; (e) Kinetics of adsorption of SIFSIX-3-Zn for pure gases and gas mixtures containing various compositions of CO2; (f) PXRD patterns of SIFSIX-2-Cu-i after multiple cycles of breakthrough tests, high pressure sorption, and water sorption experiments (compared to the calculated pattern).
FIG. 4 illustrates a scheme of a representation of the Rubotherm gravimetric-densimetric apparatus.
FIG. 5 illustrates a scheme of a representation of the Rubotherm gravimetric-densimetric-gas analysis (GDGA) apparatus for mixture gas adsorption at low and high pressure.
FIG. 6 illustrates a scheme representation of the column breakthrough experiment.
FIG. 7 illustrates a graph showing room temperature PXRD patterns of SIFSIX-2-Cu.
FIG. 8 illustrates a graph showing room temperature PXRD patterns of SIFSIX-2-Cu-i.
FIG. 9 illustrates a graph showing room temperature PXRD patterns of SIFSIX-3-Zn.
FIG. 10 illustrates a graph showing the N2 adsorption isotherms of SIFSIX-2-Cu (red) and SIFSIX-2-Cu-i (blue) at 77 K. Adsorption and desorption are represented by closed and open symbols, respectively.
FIG. 11A illustrates a graph showing low pressure isotherms at 298 K for SIFSIX-2-Cu (red) and SIFSIX-2-Cu-i (purple). FIG. 11B illustrates a graph showing CO2/N2 (10/90 mixture) and CO2/CH4 (50/50 mixture) IAST selectivity of SIFSIX-2-Cu and SIFSIX-2-Cu-i, calculated from the low pressure isotherms at 298 K. FIG. 11C illustrates a graph showing CO2Qst of SIFSIX-2-Cu and SIFSIX-2-Cu-i, estimated from low pressure isotherms at 273 and 298 K by applying the virial equation.
FIG. 12A illustrates a graph showing a column breakthrough experiment of a CO2/N2:10/90binary gas system at 298 K and 1 bar on SIFSIX-2-Cu-i. FIG. 12B illustrates a graph showing a column breakthrough experiment of a CO2/CH4:50/50 binary gas system at 298 K and 1 bar on SIFSIX-2-Cu-i. FIG. 12C illustrates a graph showing a column breakthrough experiment of a CO2/H2:30/70 binary gas system at 298 K and 1 bar on SIFSIX-2-Cu-i.
FIG. 13 illustrates a graph showing the relationship between cost of CO2 capture, CO2 selectivity, and working CO2 capacity for solid sorbents.
FIG. 14 illustrates a graph showing low pressure, variable temperature CO2 isotherms for SIFSIX-3-Zn.
FIG. 15A and FIG. 15B illustrates graphs showing high pressure single gas CO2, N2, CH4, O2, and H2 adsorption isotherms for SIFSIX-3-Zn and SIFSIX-2-Cu-I, respectively.
FIG. 16 illustrates a graph showing the experimental CO2/H2:30:70 adsorption isotherms as compared to experimental pure CO2 and H2 isotherms at 298 K for SIFSIX-3-Zn.
FIG. 17 illustrates a graph showing the fractional uptake of CO2, N2, CH4 and H2 on SIFSIX-3-Zn at 0.5 bar and 298 K.
FIG. 18 illustrates a graph showing the virial fit of CO2 isotherms of SIFSIX-2-Cu at 273 and 298 K (see FIG. 11A and FIG. 11C).
FIG. 19 illustrates a graph showing the virial fit of CO2 isotherms of SIFSIX-2-Cu-i at 273 and 298 K (see FIG. 11A and FIG. 11C).
FIG. 20 illustrates a graph showing the cyclic CO2 adsorption on SIFSIX-3-Zn using vacuum swing regeneration mode at 323 K and 0.15 bar.
FIG. 21(a) is a graph that illustrates an example of one cycle column breakthrough experiment for CO2/N2:10/90 binary gas systems at 298 K and 1 bar under dry conditions and in the presence of 74% RH carried out on SIFSIX-2-Cu-i.
FIG. 21(b) is a graph that illustrates an example of one cycle column breakthrough experiment for CO2/H2:30/70 binary gas systems at 298 K and 1 bar under dry conditions and in the presence of 74% RH carried out on SIFSIX-2-Cu-i.
FIG. 22(a) illustrates an example of one cycle column breakthrough experiment for CO2/N2:10/90 binary gas system at 298 K and 1 bar under dry conditions and in the presence of 74% RH carried out on SIFSIX-3-Zn.
FIG. 22(b) illustrates an example of one cycle column breakthrough experiment for CO2/H2:30/70 binary gas system at 298 K and 1 bar under dry conditions and in the presence of 74% RH carried out on SIFSIX-3-Zn.
FIG. 23 illustrates a graph showing PXRD patterns of SIFSIX-2-Cu-i when exposed to varying relative humidity in a nitrogen atmosphere.
FIG. 24 illustrates a graph showing VT-PXRD patterns of SIFSIX-2-Cu-i under vacuum at non-ambient temperatures (173 K-573 K).
FIG. 25 illustrates a graph showing PXRD patterns of SIFSIX-3-Zn when exposed to varying relative humidity in a nitrogen atmosphere.
FIG. 26 illustrates a graph showing the PXRD of SIFSIX-3-Zn after humidity PXRD experiment and regeneration by heating under vacuum.
FIG. 27 illustrates a graph showing the PXRD of SIFSIX-3-Zn after multiple cycles of humid breakthrough experiments and high pressure sorption experiments compared to the calculated powder pattern.
FIG. 28 illustrates a graph showing VT-PXRD patterns of SIFSIX-3-Zn under vacuum and at non-ambient temperatures (173 K-573 K).
FIG. 29 illustrates a graph showing CO2 volumetric adsorption capacity at low pressure (0-0.25 bar) and 298 K for SIFSIX-3-Zn, Mg-dobdc (313 K), UTSA-16 and SIFSIX-2-Cu-i.
FIG. 30 illustrates a graph showing water adsorption isotherm on SIFSIX-2-Cu—I and SIFSIX-3-Zn at 298 K after activation at 323 K.
FIG. 31 illustrates a graph showing GCMC-generated CO2 sorption isotherms for SIFSIX-3-Zn.
FIG. 32 illustrates a graph showing the calculations show CO2 molecules adsorbed in the pores of SIFSIX-3-Zn with the electropositive carbon atoms attracted to the SiF62-pillaring anions.
FIG. 33 illustrates a graph showing the simulated and experimental Qst plots for SIFSIX-3-Zn.
FIG. 34 illustrates a graph showing a pressure-density isotherm for CO2 at 298.15 K for the CO2 model used in this work (red) compared to experimental data (black).



DISCUSSION
Before the present disclosure is described in greater detail, it is to be understood that this disclosure is not limited to particular embodiments described, as such may, of course, vary. It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to be limiting, since the scope of the present disclosure will be limited only by the appended claims.
Where a range of values is provided, it is understood that each intervening value, to the tenth of the unit of the lower limit (unless the context clearly dictates otherwise), between the upper and lower limit of that range, and any other stated or intervening value in that stated range, is encompassed within the disclosure. The upper and lower limits of these smaller ranges may independently be included in the smaller ranges and are also encompassed within the disclosure, subject to any specifically excluded limit in the stated range. Where the stated range includes one or both of the limits, ranges excluding either or both of those included limits are also included in the disclosure.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs. Although any methods and materials similar or equivalent to those described herein can also be used in the practice or testing of the present disclosure, the preferred methods and materials are now described.
All publications and patents cited in this specification are herein incorporated by reference as if each individual publication or patent were specifically and individually indicated to be incorporated by reference and are incorporated herein by reference to disclose and describe the methods and/or materials in connection with which the publications are cited. The citation of any publication is for its disclosure prior to the filing date and should not be construed as an admission that the present disclosure is not entitled to antedate such publication by virtue of prior disclosure. Further, the dates of publication provided could be different from the actual publication dates that may need to be independently confirmed.
As will be apparent to those of skill in the art upon reading this disclosure, each of the individual embodiments described and illustrated herein has discrete components and features which may be readily separated from or combined with the features of any of the other several embodiments without departing from the scope or spirit of the present disclosure. Any recited method can be carried out in the order of events recited or in any other order that is logically possible.
Embodiments of the present disclosure will employ, unless otherwise indicated, techniques of chemistry, organic chemistry, organometallic chemistry, coordination chemistry and the like, which are within the skill of the art. Such techniques are explained fully in the literature.
The following examples are put forth so as to provide those of ordinary skill in the art with a complete disclosure and description of how to perform the methods and use the compositions and compounds disclosed and claimed herein. Efforts have been made to ensure accuracy with respect to numbers (e.g., amounts, temperature, etc.), but some errors and deviations should be accounted for. Unless indicated otherwise, parts are parts by weight, temperature is in ° C., and pressure is at or near atmospheric. Standard temperature and pressure are defined as 25° C. and 1 atmosphere.
Before the embodiments of the present disclosure are described in detail, it is to be understood that, unless otherwise indicated, the present disclosure is not limited to particular materials, reagents, reaction materials, manufacturing processes, or the like, as such can vary. It is also to be understood that the terminology used herein is for purposes of describing particular embodiments only, and is not intended to be limiting. It is also possible in the present disclosure that steps can be executed in different sequence where this is logically possible.
It must be noted that, as used in the specification and the appended claims, the singular forms “a,” “an,” and “the” include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to “a support” includes a plurality of supports. In this specification and in the claims that follow, reference will be made to a number of terms that shall be defined to have the following meanings unless a contrary intention is apparent.
General Discussion:
Embodiments of the present disclosure provide for hydrophobic multi-component metal-organic materials (MOMs) (also referred to as “hydrophobic MOM”), systems that exhibit permanent porosity and using hydrophobic MOMs to separate components in a gas, methods of separating CO2 from a gas, and the like.
Water vapor is a problem with most porous materials because it interacts strongly through chemical bonding to unsaturated metal centers or moderately through hydrogen bonding if there are hydrogen bonding sites. Porous materials that have amines grafted to their pores (for chemical bonding with CO2) also tend to react with water vapor. Embodiments of the present disclosure describe MOMs that have no unsaturated metal centers and the pore walls have no hydrogen bonding donors or acceptors, while having strong electrostatics for inducing dipoles in polarizable molecules such as CO2. In short, embodiments of the present disclosure have enhanced CO2 interactions at the same time we have reduced interactions with water vapor.
In an embodiment, the hydrophobic MOM can be porous and can be a three dimensional net so that molecules can be disposed (e.g., captured) within (e.g., pores or cavities) the hydrophobic MOM to the exclusion of other molecules. In an embodiment, the hydrophobic MOM combines sorption thermodynamics and kinetics to achieve advantageous results. For example, a gas such as CO2 is absorbed faster and stronger than other gases in the gas mixture, so that CO2 can be captured in the hydrophobic MOMs to the substantial exclusion of the other gases.
In an embodiment, the hydrophobic MOM can be used to separate CO2 from one or more other gases, where the gas includes water vapor. Due to its hydrophobic characteristic, hydrophobic MOMs can be used in methods and systems that use gases that include water vapor, which was not previously possible in porous materials that exhibit strong physisoprtion towards CO2. This is advantageous because other systems and methods that use other MOMs or other porous materials must separate water vapor from the gas prior to the gas being introduced to the other MOMs or porous materials since the other MOMs or porous materials have a higher affinity for the water vapor than CO2. If the water vapor is not removed, the other MOMs are not effective at removing CO2. Embodiments of the systems and methods can be simplified and result in reduced expenditure since the water vapor does not have to be removed prior to introduction to the hydrophobic MOMs. Even in the presence of water vapor, hydrophobic MOMs used in embodiments of the present disclosure are more effective at removing CO2 and are highly selective in separating CO2 from other gases such as N2, H2, and/or CH4.
In particular, embodiments of the present disclosure can be used in CO2 capture, gas separation, and the like, in post-combustion systems (e.g., flue gas to separate CO2 and N2), pre-combustion systems (e.g., shifted synthesis gas stream to separate CO2 and H2), and/or natural gas upgrading (e.g., natural gas cleanup to separate CO2 and CH4). In an embodiment, the hydrophobic MOMs can be used to separate other gases and can be used in processes such as He separation from natural gas, Ar separation, Kr separation, H2/D2 separation, iodine separation, and separation of unsaturated hydrocarbons from saturated hydrocarbons.
Embodiments of the present disclosure provide for hydrophobic multi-component MOMs that are three dimensional nets that have a primitive cubic topology (See FIG. 1) that can be used in methods and systems of the present disclosure. In an embodiment, the MOM can include a metal organic framework. In an embodiment, the hydrophobic MOM (e.g., [Cu (4,4′-dipyridylacetylene)2(SiF62−)]n) can be designed and synthesized using two dimensional square grids (or nets) (e.g., Cu (4,4′-dipyridylacetylene)2) that are linked via metal nodes using a pillar (e.g., SiF62−). In an embodiment, the two dimensional square grids include metal cations, metal cluster molecular building blocks (MBBs), or metal-organic polyhedral supermolecular building blocks (SBBs). The MBBs or SBBs serve the geometric role of the node in a network and they are connected by organic molecules, inorganic anions and/or metal complexes, which serve as linkers. The two dimensional square grids are connected to one another using other linkers or pillars that connect the metal nodes. In an embodiment, the components of the hydrophobic MOM (the two dimensional square grids, and its components, and pillars) can be selected to design a hydrophobic MOM that can be used in a system or method that includes water vapor and is highly effective at separating gases due to the hydrophobic MOM having a higher relative affinity for one component of the gas (e.g., CO2) over one or more other components (e.g., N2, H2, and CH4) in the gas. In this way not only is the hydrophobic MOM able to operate in methods and systems having high water vapor conditions, but the hydrophobic MOM is highly selective between or among CO2 and other components.
In an embodiment, a method of the present disclosure includes exposing a gas to a hydrophobic multi-component MOM as described herein. As noted above, the hydrophobic MOM has a greater relative affinity for a first component of the gas over a second component of the gas. The phrase “greater relative affinity” or similar phrases mean that a hydrophobic MOM will interact with a first component much more strongly than a second component so that the MOM and the first component interact to the substantial exclusion of the second component. In an embodiment, the affinity can be controlled by linkers in the hydrophobic MOM that exhibit strong enough electrostatic potential to induce polarization in one component of the gas. Thus, the first component can be captured (e.g., separated) from the gas mixture to form a modified gas, where the modified gas includes the second component and a substantially reduced amount (e.g., greater than about 80% or more, about 90% or more, about 95% or more, about 99% or more, about 99.9% or more, removal of the first component from the gas) of the first component.
As described herein, a substantial advantage of embodiments of the present disclosure is that methods and systems using the hydrophobic MOMs can be conducted using a gas having water vapor, which is a completely unexpected result since other MOMs and related inorganic porous materials are typically hydrophilic and have a strong affinity for water so that the water vapor needs to be substantially or completely removed from the gas for the MOM to be commercially viable. In an embodiment, the water vapor in the gas can be at a concentration of about 1% to 10% at a temperature of about 273K to 340K.
In an embodiment, the gas can include two or more components and includes water vapor. In an embodiment, gas does not include water vapor. In an embodiment, the component can include one or more of the following: CO2, N2, H2, CH4, He, hydrocarbons having 2 or more carbons (saturated or unsaturated and/or linear or branched), and a combination thereof. In an embodiment, CO2 can be in the gas in an amount of about 400 ppm to 50%. In an embodiment, N2 can be in the gas in an amount of about 50% to 99.99%. In an embodiment, H2 can be in the gas in an amount of about 50% to 99.99%. In an embodiment, CH4can be in the gas in an amount of about 50% to 99.99%. In an embodiment, He can be in the gas in an amount of about 50% to 99.99%.
It should be noted that in many situations, the gas may primarily include a few components or only a few components that are important to the desired separation. For example, in post-combustion systems such as one that contains flue gas, the two main components (e.g., in the presence of water vapor) for separation are CO2 and N2. In another example, in pre-combustion systems such as shifted synthesis gas streams, the two main components to separate are CO2 and H2. In another embodiment, in natural gas upgrading systems such as natural gas cleanup, the two main components to separate are CO2 and CH4. In another embodiment, in a He separation system, the two main components to separate are He and natural gas.
In an embodiment, the components in a gas can be separated using a system to introduce the gas to the hydrophobic MOM and remove the modified gas. In an embodiment, a first structure or device including the hydrophobic MOM can be interfaced with a second structure or device to introduce a gas to the first structure so that the gas and the hydrophobic MOM can interact so that the hydrophobic MOM can capture the first component (e.g., CO2). After a sufficient period of time and under appropriate temperature conditions, the remaining gas or modified gas can be removed from the first structure. This process can be repeated as appropriate for the particular system. After a period of time, the first component can be removed from the hydrophobic MOM and the hydrophobic MOM can be reused and/or recycled using an appropriate gas handling system.
In an embodiment, the first structure and the second structure can include those used in systems such as post-combustion systems, pre-combustion systems, natural gas upgrading systems, and He separation systems. In particular, the first structure can include structures such as those used in typical systems mentioned above. In an embodiment, the second structure can include standard gas handling systems, valves, pumps, flow meters, and the like.
As mentioned above, the separation method or system using the hydrophobic MOMs can be used to selectively remove CO2 from N2, H2, and/or CH4. In an embodiment, the selectivity for CO2/N2 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on ideal absorbed solution theory (IAST) calculations (described in greater detail in the Example) and at conditions similar to those described in the Example. In an embodiment, the selectivity for CO2/N2 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on breakthrough experiments (described in greater detail in the Example) and at conditions of similar to those described in the Example.
In an embodiment, the selectivity for CO2/H2 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on IAST calculations and at conditions similar to those described in the Example. In an embodiment, the selectivity for CO2/H2 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on breakthrough experiments (described in greater detail in the Example) and at conditions of similar to those in the Example.
In an embodiment, the selectivity for CO2/CH4 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on based on IAST calculations and at conditions of similar to those described in the Example. In an embodiment, the selectivity for CO2/CH4 can be about 100 or more, about 500 or more, about 1000 or more, or about 2000 or more, based on breakthrough experiments (described in greater detail in the Example) and at conditions of similar to those described in the Example.
As noted above, hydrophobic MOMs can be three dimensional nets that can have a primitive cubic topology but they could also exhibit a different topology (See FIG. 1). In an embodiment, the hydrophobic MOM can be designed and synthesized using two dimensional square nets that are linked via metal nodes using a molecule or ion that serves the role of a pillar. In an embodiment, the two dimensional square nets can include metal cations, MBBs, or SBBs, and linkers can be used to bond the metal ions and the MBB and the SBB.
In an embodiment, hydrophobic MOMs can have one of the following generic structures: (M(L)a(P)n), where M is the metal ion, L is the linker, and P is the pillar, a is 2 and n is 1. L and P can be difunctional ligands that are capable of linking the metal clusters or ions such as pyrzazine, 4,4′-bipyridine, 1,4-benzenedicarboxylate, hexafluorosilicate, and hexafluorotitanate. In an embodiment, these types of hydrophobic MOMs are described in references 13-15 below in the Example, which are incorporated herein by reference for how to describe MOMs and MOFs and the components of each.
In an embodiment, the metal cations can include M1+ (e.g., Na, K, Li, Ag, etc.); M2+ (e.g., Cu, Zn, Co, Mn, Mo, Cr, Fe, Ca, Ba, Cs, Pb, Pt, Pd, Ru, Rh, Cd, etc.); M3+ (e.g. In, Fe, Y, Ln (Yb, Tb, etc.)); M4+ (e.g., Zr, Ti, V, etc.); or other higher oxidative state metals such as +4, +5, +6, +7, and +8. In an embodiment, the MBBs and SBBs can include these metal cations as well.
In an embodiment, the linkers in the two dimensional square grid can include organic molecules, inorganic anions and/or metal complexes. In an embodiment, the linkers can include pyrazine (substituted and unsubstituted) and derivatives thereof, bipyridine (substituted and unsubstituted) and derivatives thereof, and the like.
In an embodiment, the pillars can include organic molecules, inorganic anions and/or metal complexes. In an embodiment, the pillars can include SiF62−, GeF62−, TiF62−, SnF62−, PF6−, and NO3−.
In an embodiment, the hydrophobic MOM can include: [Cu(4,4′-dipyridylacetylene)2(SiF6)]n, where n is 1 to 100,000,000; a pair of interpenetrated nets of [Cu(4,4′-dipyridylacetylene)2(SiF6)]n; and {[Zn(pyr)2(SiF6)]n, wherein n is 1 to 100,000,000.
EXAMPLE
Now having described the embodiments of the present disclosure, in general, the Examples describe some additional embodiments of the present disclosure. While embodiments of present disclosure are described in connection with the Examples and the corresponding text and figures, there is no intent to limit embodiments of the present disclosure to these descriptions. On the contrary, the intent is to cover all alternatives, modifications, and equivalents included within the spirit and scope of embodiments of the present disclosure.
Example 1
Brief Introduction
The energy costs associated with the separation and purification of industrial commodities such as gases, fine chemicals and fresh water currently consumes around 15% of global energy production and the demand for such commodities is projected to triple by 20501. The challenge of developing effective separation and purification technologies that exhibit a much smaller energy footprint is pronounced with CO2, which, in addition to its notoriety with climate change, is an impurity in natural gas, biogas, syngas and many other gas streams. In such a context, porous crystalline materials that can exploit both equilibrium and kinetic selectivity, size selectivity and targeted molecular recognition, are attractive targets for CO2 separation and capture as exemplified by zeolites 5A and 13X2, as well as Metal-Organic Materials (MOMs)3-9. Here we report that a crystal engineering′ or reticular chemistry5,9 strategy that controls pore functionality and size in a series of MOMs with coordinately saturated metal centers and periodically arrayed SiF62− (SIFSIX) anions enables a “sweet spot” of kinetics and thermodynamics that offers high volumetric uptake at low CO2 partial pressure (<0.15 bar) and most importantly an unprecedented CO2 sorption selectivity over N2, H2 and CH4 even in the presence of moisture. These MOMs are therefore relevant to CO2 separation in the context of post-combustion (flue gas CO2/N2), pre-combustion (shifted synthesis gas stream CO2/H2) and natural gas upgrading (natural gas cleanup CO2/CH4).
Example Discussion:
Porous materials with unsaturated metal centers (UMCs)10 or organic amines that chemically interact with CO2 enhance selectivity for CO2 in the presence of other gases. However there are drawbacks: high energy costs associated with activation, regeneration and recycling of the sorbent material, especially for amines11; competition with water vapor, especially for UMCs12; selectivity tends to monotonically decrease with increased loading of sorbate. Consequently, there remains a need for sorbents with favorable CO2 sorption kinetics and thermodynamics over a wide range of CO2 loading that would permit efficient CO2 capture with low regeneration costs. MOMs are attractive in this context because they are inherently modular, i.e. metals or metal clusters (“nodes” or “molecular building blocks”) coordinated to multi-functional organic ligands (“linkers”), and they offer extra large surface areas up to 7000 m2/g.6 However, although extra-large surface area facilitates high gravimetric uptake of gases at low temperature and/or high pressure, it is not necessarily conducive to efficient separations under practical conditions. We herein address how to optimize the thermodynamics and kinetics of gas adsorption through a class of MOMs that is amenable to crystal engineering or isoreticular chemistry in a manner that facilitates exquisite control over pore size and functionality: “pillared grids”, 2D nets based upon linked metal nodes that are pillared in the 3rd dimension to form 3D nets with primitive cubic (pcu) topology13. [Cu(4,4′-bipyridine)2(SiF6)], a prototypal pcu net that remains one of the best sorbents for CH4 as measured by volumetric uptake14, exhibits highly selective CO2 uptake vs. both CH4 and N2 at 1 bar and 298 K15. In the absence of UMCs or amine groups, we attributed this behavior to favorable CO2-SIFSIX interactions. This compound, SIFSIX-1-Cu, exhibits 1D square channels (pore size 8.5 Å) aligned by a periodic array of SIFSIX pillars and is prototypal for a class of compounds that is amenable to pore-size tuning. In this contribution we report the synthesis, structure and remarkable sorption properties of three variants of SIFSIX-1-Cu with expanded and contracted pore sizes.
Reaction of 4,4′-dipyridylacetylene, dpa16 with CuSiF6 afforded purple rod-shaped crystals of SIFSIX-2-Cu {[Cu(dpa)2(SiF6)]n} (see Supporting Information for synthetic and crystallographic details for this and other compounds reported herein). SIFSIX-2-Cuforms the expected pcu net with square channels of pore dimensions 10.5×10.5 Å2 (FIG. 1a). The interpenetrated polymorph, SIFSIX-2-Cu-i, is composed of doubly interpenetrated nets that are isostructural to the nets in SIFSIX-2-Cu. The independent nets are staggered with respect to one another affording 4.9 Å pores if measured diagonally (FIG. 1b). SIFSIX-3-Zn, {[Zn(pyr)2(SiF6)]n}, was prepared according to published procedures17 and is also a pcu net which encloses 3.9×3.9 Å2 channels (FIG. 1c). Pore sizes in this series therefore range from ultramicroporous to nanoporous. Bulk purity was confirmed using powder x-ray diffraction patterns (PXRD) (FIGS. 7-9).
Pure Gas Adsorption Studies. Sub-atmospheric pressure gas adsorption studies of H2, CO2, CH4, and N2 are detailed in Table 1. Activation of SIFSIX-2-Cuand SIFSIX-2-Cu-i (evacuation at 295K for 12 hours) afforded BET apparent surface areas of 3140 and 735 m2/g, respectively, (corresponding Langmuir values 3370 and 821 m2/g) from N2 adsorption isotherms at 77 K. Micropore volumes are in good agreement with corresponding theoretical values (FIG. 10 and Table 3, Supplemental section). SIFSIX-3-Zn adsorbs minimal amounts of N2 at 77 K and thus its surface area (250 m2/g) was determined from the CO2 isotherm collected at 298 K18.







TABLE 1







Summary of single gas and gas mixture adsorption results compared to


those for Mg-dobdc and zeolite 13X.











Compounds















SIFSIX-2-Cu
SIFSIX-2-Cu-i
SIFSIX-3-Zn
Mg-dobdcf
13Xg















Pore size(Å)
13.05
5.15
3.84
10.8
10


CO2Qst at low CO2 loading
22
31.9
45
47-52
44-54


(kJ/mol)







Single CO2 uptake (298K)
 10/81.3
 76/238
105/112
220/352
106/220


(mg/g) at 0.1 bar/1 bar







Single CO2 uptake (298K)
3/26
 48/151
84/90
101/162
 61/126


(cm3/cm3) at 0.1 bar/1 bar







Single CH4 uptake (298K)
6.2
7.5
12.6
17.8
4.2


(mg/g) at 1 bar







Single N2 uptake (298K)
4.9
4.2
6.4
na
6.4


(mg/g) at 1 bar







Single H2 uptake (298K)
nm
0.2
1.37
na
na


(mg/g) at 1 bar







CO2 uptake (298K) in
8.4a
70a/55b
 99.9a/104.4d
na
na


CO2/N2:10/90 mixture at 1







bar







(mg/g)







CO2 uptake (298K) in
42.8a
183a/138b
108a/110d
na
na


CO2/CH4:50/50 mixture at 1







bar (mg/g)







CO2 uptake (298K) in
nm
—/85b
—/112c
na
na


CO2/H2:30/70 mixture at 1







bar (mg/g)


















Selectivity
CO2/N2
13.7a
140a/72b 
1818a/1700d
na
420a


at 1 bar
CO2/CH4
5.3a
33a/51b
231a/350d
137a
103a



CO2/H2
nm
240b
>1800
800f
na





aIAST;


bbreakthrough experiments;


cmixture gravimetric (G) experiment;


dmixture gravimetric-densimetric gas analysis (GDGA) experiment;


edue to the high error associated with H2 adsorption measurements (very low uptake), quantitative measurement of CO2/H2 was not possible;


fLong et al. 2011 (313K data);


gCavenati et al. 2004 (298K data);


na: not available;


nm: not measured.






Low pressure CO2, CH4, and N2 sorption data were collected at 298 K (FIG. 11a, Table 1). SIFSIX-2-Cu exhibited CO2 uptake of 41.4 cm3 g−1 (1.84 mmol g−1; 81.3 mg g−1) at 298 K and 1 bar but its denser polymorph, SIFSIX-2-Cu-i, exhibited substantially higher values of 121.2 cm3 g−1(5.41 mmol g−1; 238 mg g−1). Such behavior has also been observed in the context of hydrogen adsorption19. A review of the literature reveals that the gravimetric CO2 uptake of SIFSIX-2-Cu-i at 298 K and 1 bar is among the highest yet reported (e.g. Mg-dobdc10, Co-dobdc10, MIL-10120, [Cu(Me-4py-trz-ia)]21and partially hydrated HKUST-122). Notably, these MOMs possess higher surface area, are less dense than SIFSIX-2-Cu-i and contain UMCs. Volumetric CO2 uptake of SIFSIX-2-Cu-i at atmospheric pressure approaches that of Mg-dobdc (151 vs.163 v/v). Ideal Adsorbed Solution Theory (IAST)23 calculations indicate binary gas adsorption selectivity (FIG. 11b) under practically relevant conditions (298 K; CH4 and N2 mole fractions equal to 0.5 and 0.9, respectively) to be dramatically higher for SIFSIX-2-Cu-i than SIFSIX-2-Cu for both CO2/CH4 (33 vs. 5.3) and CO2/N2 (140 vs. 13.7). These findings agree with the CO2/CH4 (51) and CO2/N2 (72) adsorption selectivity determined experimentally for SIFSIX-2-Cu-i using column breakthrough tests (FIG. 12). To the best of our knowledge, the CO2/CH4 and CO2/N2 IAST selectivity exhibited by SIFSIX-2-Cu-i are the highest yet reported for a MOM without UMCs or amino groups. We attribute these observations to the enhanced isosteric heat of adsorption (Qst) of SIFSIX-2-Cu-i vs. SIFSIX-2-Cu (45% higher at minimum loading, 71.5% greater at 2.8 mmol g−1, FIG. 11c). This increase is presumably attributable to better overlap of attractive potential fields of opposite walls in the relatively narrower pores of SIFSIX-2-Cu-i. SIFSIX-2-Cu-i is also suitable for CO2 separation from syngas thanks to its CO2/H2:30/70 selectivity (240) as determined from column breakthrough experiments (FIG. 12c).
The heart of pressure and temperature swing adsorption processes (PSA and TSA) for CO2 removal is the adsorbent bed and a recent study projected that a CO2/N2 selectivity of >500 combined with a capacity of 2 to 4 mmolg−1 for a CO2/N2:10/90 mixture would be required for practical utility (FIG. 13).24 FIGS. 2a and 2b present the CO2 adsorption isotherms of SIFSIX-2-Cu-i and SIFSIX-3-Zn, respectively, collected at sub-atmospheric pressures after activation at 298 K. Contraction of the pores led to a sharp increase in CO2 uptake at low CO2 loading with nearly 11 wt % at 0.1 bar for SIFSIX-3-Zn vs. 4.4 wt % at 0.1 bar for SIFSIX-2-Cu-i. Notably, the CO2 uptake for SIFSIX-3-Zn reached saturation at relatively low pressures (ca. 0.3 bar; FIG. 14) while the CO2 adsorption isotherm on SIFSIX-2-Cu-i reached a plateau at relatively higher pressures (5-7 bar) (FIG. 15b). As a result, SIFSIX-3-Zn exhibits high volumetric CO2 uptake that is comparable to those of Mg-dobdc10 and UTSA-1625 at a CO2 partial pressure typical for post-combustion CO2 capture (FIG. 29).
FIG. 2c presents the Qst of CO2 adsorption for SIFSIX-2-Cu-i and SIFSIX-3-Zn from variable temperature isotherms (FIG. 2a, b) and the Qst of up to 45 kJ mol−1 is consistent with the steepness of the CO2 isotherms. The relatively constant Qst indicates homogenous binding sites over the full range of CO2 loading (FIG. 2c). These Qst values are in the “sweet spot” favorable for efficient, reversible adsorption-desorption, i.e. strong but still reversible and are supported by modeling studies (FIGS. 2d, 31-33).
The CO2 selectivity of SIFSIX-3-Zn was investigated via column breakthrough tests using binary CO2/N2:10/90 (FIG. 2e) and CO2/CH4:50/50 gas mixtures (FIG. 2f) at 298 K and atmospheric pressure and compared to the corresponding breakthrough tests on SIFSIX-2-Cu-i. Remarkably, SIFSIX-3-Zn showed much higher selectivity (495 and 109 for CO2/N2:10/90 and CO2/CH4:50/50, respectively) than SIFSIX-2-Cu-i as CO2 was retained for longer times (e.g., ca. 2000 sec vs. 300 sec for CO2/N2). Markedly, N2 and CH4 breakthrough occurred within seconds. In order to support and confirm the high selectivity derived from the breakthrough experiments, single gas (CO2, N2, CH4 and H2) sorption isotherms were conducted at low and high pressures and IAST calculations were used to predict CO2/CH4:05/95, CO2/CH4:50/50, CO2/N2:10/90 and CO2/H2:30/70 binary mixture adsorption equilibria. These mixtures mimic natural gas upgrading, biogas treatment, post- and pre-combustion capture applications, respectively.
Gas Mixture Adsorption Studies. FIGS. 3a and 3b reveal that the CO2 adsorption selectivity of SIFSIX-3-Zn calculated for binary gas separation vs. CH4 and N2 is unprecedented, outperforming Mg-dobdc10, UTSA-1625, and zeolite 13X26. Indeed, SIFSIX-3-Zn compares to amine-functionalized MOFs27 and amine-bearing mesoporous silica28, particularly at low CO2 partial pressure. The extraordinary calculated selectivity for CO2/N2 (i.e. 1539±307 at 1 bar and 298 K) was validated by gas mixture gravimetric adsorption experiments at various pressures (FIG. 3c, d).
With regards to CO2/H2 mixtures, adsorption isotherms of CO2/H2:30/70 were collected and showed similar shape and uptake to that obtained using pure CO2 (FIG. 16). This indicates that SIFSIX-3-Zn adsorbs CO2 with very large selectivity over H2 containing mixtures (higher than 1800), making it potentially suitable for pre-combustion capture or H2 purification. Because of the large error associated with H2 adsorption measurement (relatively low uptake) quantitative measurements of CO2/H2 selectivity was not possible. We note that calculated and measured selectivity exceeding 1000 are often subject to uncertainties associated with measurement of the gas uptake of weakly adsorbed gases. Therefore, it would be inappropriate in this case to make quantitative comparisons between different adsorbents such as SIFSIX-3-Zn and Mg-dobdc29 (800 at 1 bar and 313 K).
In order to confirm the synergistic nature of the thermodynamics and kinetics for CO2 capture, competitive adsorption kinetic studies using the above gas mixtures were conducted and are presented in FIG. 3e. Interestingly, the uptake at equal times for CO2/N2, CO2/CH4 and CO2/H2 mixtures follow the behavior of pure CO2. In addition, at equilibrium the total uptake of the CO2 containing gas mixtures overlay perfectly with the equilibrium uptake for pure CO2. These unprecedented findings show that when CO2 containing mixtures are contacted with SIFSIX-3-Zn, CO2 adsorbs more strongly and faster than N2, O2, CH4 and H2, thus occupying all the available space and sorption sites and consequently excluding other gases. Most importantly, SIFSIX-3-Zn fulfills the demanding attributes (FIG. 13) required for economical and efficient CO2 post-combustion separation. Further, increasing the adsorption temperature did not significantly reduce the steepness of the CO2 adsorption isotherm for SIFSIX-3-Zn (FIGS. 2b, 14), a desirable feature in many CO2 separation and purification applications.
Recyclability and Effect of Moisture.
Whereas the sorbents reported herein exhibit exceptional performance with respect to CO2 selectivity, their amenability to recycling and efficacy in the presence of moisture must also be addressed. Recyclability was validated via adsorption-desorption cycle experiments conducted at 323 K and 0.15 bar (FIG. 20). The impact of water vapor on the CO2 capacity and selectivity for SIFSIX-2-Cu-i and SIFSIX-3-Zn was evaluated via a series of adsorption measurements. Water vapor adsorption isotherms are type I isotherms with uptakes of 20 wt % and 11 wt %, respectively, at 74% RH (FIG. 30). Water adsorption affinity/capacity is reduced in the presence of CO2 gas mixtures as revealed by breakthrough experiments, especially for SIFSIX-3-Zn (FIGS. 21b and 22b). Importantly, the presence of water in the given gas mixture had a negligible effect at elevated CO2 concentrations (FIG. 21b) in the case of SIFSIX-2-Cu-i. Regarding the CO2/H2:30/70 mixture, CO2 uptake and selectivity were only slightly reduced in the presence of moisture (1.61 mmol/g and 191 at 74% RH vs. 1.99 mmol/g and 237 at 0% RH for SIFSIX-2-Cu-i, FIG. 21b). Whereas SIFSIX-2-Cu-i was structurally unchanged by exposure to moisture (FIG. 3f), SIFSIX-3-Zn undergoes a reversible phase change at relatively high humidity (FIGS. 25-28).
In conclusion, we demonstrate how a crystal engineering or reticular chemistry approach to pore size control coupled with favorable electrostatics from an array of inorganic anions affords porous materials with exceptional selectivity, recyclability and moisture stability in the context of several industrially relevant CO2 separation applications. In effect, the structural features and exceptional mixed gas sorption properties of the SIFSIX compounds reported herein reveal that is now possible to combine equilibrium10,11,26 and kinetic30 adsorption selectivity in the same porous material to facilitate effective CO2 separation and capture.
References, each of which is incorporated herein by reference:


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Supplemental Information for Example 1:

1—Ligand and MOM Synthesis:

    All chemicals with the exception of 1,2-bis(4-pyridyl)acetylene (dpa) were obtained commercially and used as received without further purification. Synthesis of dpa was accomplished by minor modification of a previously reported procedure.1 1,2-bis(4-pyridyl)acetylene, dpa:
    Br2 (3.5 mL, 10.8 g, 68 mmol) was added dropwise to a stirred solution of trans-1,2-bis(4-pyridyl)ethylene (3.52 g, 19.3 mmol) in HBr (48%, 46.5 mL) at 0° C.
    The mixture was stirred at 120° C. for 2 hours and subsequently cooled to room temperature yielding an orange precipitate. After chilling in ice for 30 min. the solid was filtered, washed with water, and then stirred in aqueous NaOH (2 M, 120 mL) for 30 min. The resulting white solid, 1,2-dibromo-1,2-bis(4-pyridyl)ethane, was filtered, washed with 250 mL of water, and dried under vacuum for 24 hours (yield 5.1 g, 77%). Finely cut Na (2.2 g, 96 mmol) was stirred in t-BuOH (120 mL, dried over 4 Å molecular sieves) at 80° C. under nitrogen until dissolution (20 hrs.). 1,2-dibromo-1,2-bis(4-pyridyl)ethane (4.0 g, 11.7 mmol) was added in portions and the mixture was stirred under nitrogen at 80° C. for 4 hrs. The mixture was next cooled to room temperature and EtOH was added (20 mL), followed by water (20 mL, CAUTION!). The brown solution was extracted with CHCl3 until the extracts became colorless (ca. 4×70 mL) and then the CHCl3 was evaporated to give a brown solid, which was recrystallized from toluene (overall yield 43%).

SIFSIX-2-Cu, {[Cu(dpa)2(SiF6)]n}



Synthesis: Room temperature diffusion of an ethanol solution of dpa (2 mL, 0.115 mmol) into an ethylene glycol solution of CuSiF6 (2 mL, 0.149 mmol) produced purple rod-shaped crystals of SIFSIX-2-Cu after 2 weeks in 87.4% yield (based on dpa).
SIFSIX-2-Cu-i, {[Cu(dpa)2(SiF6]n.2.5CH3OH}
Synthesis: Blue plate single crystals of SIFSIX-2-Cu-i were synthesized in 99.8% yield (based on dpa) by room temperature diffusion of a methanol solution of CuSiF6 (2 mL, 0.149 mmol) into a DMSO solution of dpa (2 mL, 0.115 mmol) for 1 week. An alternative direct mixing method was used to produce powdered samples of SIFSIX-2-Cu-i. A methanol solution of dpa (4 mL, 0.270 mmol) was stirred with an aqueous solution of CuSiF6 (4 mL, 0.258 mmol) resulting in a purple precipitate, which was then heated at 85° C. for 12 hrs (83.3% yield based on dpa).
SIFSIX-3-Zn, {[Zn(pyr)2(SiF6)]n},
SIFSIX-3-Zn was synthesized using a previously known procedure at room temperature by diffusion of a methanol solution of pyrazine (2 mL, 1.3 mmol) into a methanol solution of ZnSiF6 (2 mL, 0.6 mmol). Crystals were harvested after 3 days.
2—Low Pressure Gas Sorption Measurements:
Crystalline samples of SIFSIX-2-Cu-i and SIFSIX-3-Zn were activated for low pressure gas sorption analysis by washing the as-synthesized material with DMF followed by solvent exchange in methanol (MeOH) for 3 days. Each of the activated samples (80-160 mg) were transferred to a pre-weighed 6-mm large bulb glass sample cell and evacuated at room temperature for 92 hours (SIFSIX-2-Cu-i) and 25 hours (SIFSIX-3-Zn) on an Autosorb-1C (Quantachrome Instruments) low-pressure adsorption instrument, equipped with a turbo molecular vacuum pump. The low pressure gas sorption isotherms in FIG. 11 were collected on an ASAP 2020 Surface Area and Porosity Analyzer (Micromeritics) after activation of SIFSIX-2-Cu and SIFSIX-2-Cu-i as follows. As-synthesized SIFSIX-2-Cu was exchanged with 1:1 ethylene glycol/ethanol for 3 days and then ethanol for 5 days. The sample was degassed at room temperature under high vacuum (<5 μm Hg) for 16 hours prior to sorption analysis. During evacuation a color change from dark purple to aqua blue was observed. SIFSIX-2-Cu-i (synthesized by direct mixing) was activated by solvent exchange in MeOH for 3 days followed by evacuation at room temperature for 16 hours, during which time a color change from light purple to light blue occurred.
The apparent surface areas of SIFSIX-2-Cu-i and SIFSIX-3-Zn were determined from the nitrogen adsorption isotherm collected at 77 K and the CO2 adsorption isotherm collected at 298 K, respectively by applying the Brunauer-Emmett-Teller (BET) and Langmuir models. The determination of the isosteric heat of adsorption (Qst) for CO2 in FIG. 2c was estimated by applying the Clausius-Clapeyron expression using the CO2 sorption isotherms measured at 258, 273, 288 and 298 K for SIFSIX-2-Cu-i and 298, 308, 318, 328 and 338 K for SIFSIX-3-Zn. The bath temperature was precisely controlled using a Julabo recirculating control system containing a mixture of ethylene glycol and water. Data points below 0.76 Torr were not used for this calculation, in order to avoid possible artifacts at very low coverage. The Qst curves in FIG. 11c were estimated by applying the virial equation to the CO2 isotherms at 273 and 298 K (FIGS. 18 and 19).
3—High Pressure Single Gas and Binary Gas Sorption Procedure and Measurements:
Single Gas Sorption (Gravimetric Technique)
Adsorption equilibrium measurements of pure gases were performed using a Rubotherm gravimetric-densimetric apparatus (Bochum, Germany) (Scheme S1), composed mainly of a magnetic suspension balance (MSB) and a network of valves, mass flowmeters and temperature and pressure sensors. The MSB overcomes the disadvantages of other commercially available gravimetric instruments by separating the sensitive microbalance from the sample and the measuring atmosphere and is able to perform adsorption measurements across a wide pressure range, i.e. from 0 to 20 MPa. The adsorption temperature may also be controlled within the range of 77 K to 423 K. In a typical adsorption experiment, the adsorbent is precisely weighed and placed in a basket suspended by a permanent magnet through an electromagnet. The cell in which the basket is housed is then closed and vacuum or high pressure is applied.
The evacuated adsorbent is then exposed to a continuous gas flow (typically 50 ml/min) or static mode at a constant temperature. The gravimetric method allows the direct measurement of the reduced gas adsorbed amount Ω. Correction for the buoyancy effect is required to determine the excess adsorbed amount using equation 1, where Vadsorbent and Vss refer to the volume of the adsorbent and the volume of the suspension system, respectively. These volumes are determined using the helium isotherm method by assuming that helium penetrates in all open pores of the materials without being adsorbed. The density of the gas is determined experimentally using a volume-calibrated titanium cylinder. By weighing this calibrated volume in the gas atmosphere, the local density of the gas is also determined. Simultaneous measurement of adsorption capacity and gas phase density as a function of pressure and temperature is therefore possible. The excess uptake is the only experimentally accessible quantity and there is no reliable experimental method to determine the absolute uptake. For this reason, only the excess amounts are considered in this work.

Ω=mexcess−ρgas(Vadsorbent+Vss)  (1)

    The pressure is measured using two Drucks high pressure transmitters ranging from 0.5 to 34 bar and 1 to 200 bar, respectively, and one low pressure transmitter ranging from 0 to 1 bar. Prior to each adsorption experiment, about 100 mg to 300 mg sample is outgassed at 433 K at a residual pressure 10−4 mbar. The temperature during adsorption measurements is held constant by using a thermostated circulating fluid.

Mixture Gas Adsorption (Gravimetric-Densimetric-Gas Analysis Technique)



Adsorption measurements of binary gas mixtures were carried out using a Rubotherm gravimetric-densimetric technique coupled to a gas analyzer (gas chromatography (GC) or mass spectrometery (MS)) (Scheme S2) enabling accurate measurements of mixture gas adsorption in the pressure range of 0-10 bar. The gas dosing system comprise there mass flow controllers (MFC) for gas premixing. Premixed gases can be also supplied. The adsorbent sample (up to 2 g) is placed in a sample a closed holder to prevent blowing the fine powder samples during gas expansion from the dosing cell to adsorption cell, and out gassed at a maximum temperature of 298 K before the actual adsorbent mass is measured.
At the beginning of an experiment, the whole installation is under vacuum, and then the premixed gas is supplied to the first dosing volume (V1) while the adsorption cell kept isolated (V4 and V6 closed). Knowing the dosing volume, the pressure and the temperature and using an appropriate (p−v−T) equation of state (EOS) the amount of gas introduced can be determined and controlled to match the amount of adsorbent available for analysis which is a critical factor influencing the accuracy of the set-up. The circulation pump is switched on to homogenize the gas mixture. The system allows checking the initial gas composition by sampling the premixed gas to the gas analysers. Once the mixture is completely homogeneous it is directed in the adsorption cell by opening valves V4 and V6 then the circulation pump is switched on. Once the adsorption equilibrium is reached, the circulation pump is switched off and the mass is monitored with the magnetic balance, the mass being recorded every 10 min. If the standard deviation is under 50 μg, the value is recorded; otherwise, the circulation pump is switched on for additional time and the control of equilibrium state is repeated. When the mass is stable, the mass, temperature and pressure are then recorded. Valve V11 is then opened and the gas phase after adsorption analyzed by GC or MS. Using an appropriate (p−v−T) EOS for the studied mixture, in addition to the pressure, temperature and gas mixture composition after adsorption, the number of mole adsorbed of compound 1 can be calculated using equation (2):




  
    
      
        
          n
          
            1
            ⁢
            
              
            
            ⁢
            ads
          
        
        =
        
          
            
              
                
                  P
                  ·
                  
                    V
                    1
                  
                  ·
                  
                    y
                    1
                    ′
                  
                
                
                  R
                  ·
                  T
                
              
              +
              
                
                  y
                  1
                
                ·
                
                  (
                  
                    
                      
                        m
                        ads
                      
                      
                        M
                        2
                      
                    
                    -
                    
                      
                        P
                        ·
                        
                          V
                          1
                        
                        ·
                        
                          y
                          1
                          ′
                        
                      
                      
                        R
                        ·
                        T
                      
                    
                    -
                    
                      
                        P
                        ·
                        
                          V
                          1
                        
                        ·
                        
                          y
                          2
                          ′
                        
                      
                      
                        R
                        ·
                        T
                      
                    
                  
                  )
                
              
            
            
              1
              +
              
                
                  y
                  1
                
                ·
                
                  (
                  
                    
                      
                        M
                        1
                      
                      
                        M
                        2
                      
                    
                    -
                    1
                  
                  )
                
              
            
          
          ·
          
            1
            
              m
              sample
            
          
        
      
    
    
      
        (
        2
        )
      
    
  




Where:

n1ads adsorbed amount of compound 1,

P: pressure in the dosing cell

V1 volume of the dosing cell

y′1: gas phase composition before adsorption

y1: gas phase composition after adsorption of compound 1

T: temperature

R: ideal gas constant

mads: total adsorbed amount in mg

M1: Molecular weight of compound 1

M2: Molecular weight of compound 2

msample mass the evacuated sample

The number of mole adsorbed of compound 2 n2ads is calculated using equation 3:





  
    
      
        
          n
          
            2
            ⁢
            
              
            
            ⁢
            ads
          
        
        =
        
          
            
              m
              adstotal
            
            
              
                
                  M
                  1
                
                ·
                
                  y
                  1
                
              
              +
              
                
                  M
                  2
                
                ·
                
                  y
                  2
                
              
            
          
          -
          
            n
            
              ads
              ⁢
              
                
              
              ⁢
              1
            
          
        
      
    
    
      
        (
        3
        )
      
    
  




The adsorbed phase composition of compound 1 and 2 is then calculated using equations 4 and 5:





  
    
      
        
          
            x
            1
          
          =
          
            
              n
              
                1
                ⁢
                
                  
                
                ⁢
                ads
              
            
            
              n
              adstot
            
          
        
        ;
      
    
    
      
        (
        4
        )
      
    
  
  
    
      
        
          x
          2
        
        =
        
          
            n
            
              2
              ⁢
              
                
              
              ⁢
              ads
            
          
          
            n
            adstot
          
        
      
    
    
      
        (
        5
        )
      
    
  




The selectivity of compound 2 over 1 is then calculated using equation 6:





  
    
      
        
          S
          
            2
            /
            1
          
        
        =
        
          
            
              x
              2
            
            /
            
              x
              1
            
          
          
            
              y
              2
              ′
            
            /
            
              y
              1
              ′
            
          
        
      
    
    
      
        (
        6
        )
      
    
  




4—Column Breakthrough Test Set-Up, Procedure and Measurements:

The experimental set-up used for dynamic breakthrough measurements is shown in Scheme S3. The gas manifold consisted of three lines fitted with mass flow controllers Line “A” is used to feed an inert gas, most commonly helium, to activate the sample before each experiment. The other two lines, “B” and “C” feed a mixture of CO2 and other gases like N2, CH4, H2. Hence, gas mixtures with concentrations representative of different industrial gases may be prepared. Whenever required, gases flowing through lines “B” and “C” may be mixed before entering a column packed with SIFSIX-2-Cu-i and SIFSIX-3-Zn using a four-way valve. The stainless steel column was 27 mm in length with 4 mm of inner (6.4 mm outer) diameter. The column downstream was monitored using a Hideen mass spectrometer. In a typical experiment, 0.1-0.4 g of adsorbent was treated at 298 K overnight under helium flow of 5 mL/min, then the gas flow was switched to the desired gas mixture at the same flow rate. The complete breakthrough of CO2 and other species was indicated by the downstream gas composition reaching that of the feed gas. Experiments in the presence of 74% relative humidity were performed by passing the gas mixture through water vapor saturator at 20° C.
The adsorption capacity for each compound was estimated from the breakthrough curves using the following equation:

nadsi=FCiti  (7)

where nadsi is the adsorption capacity of the compound i, F is the total molar flow, Ci is the concentration of compound i entering the column and ti is the time corresponding to compound i, which is estimated from the breakthrough profile.
The selectivity of CO2 over species i in the binary mixture of CO2 and species i is determined using the following equation:




  
    
      
        
          S
          
            C
            ⁢
            
              
            
            ⁢
            
              
                O
                2
              
              /
              i
            
          
        
        =
        
          
            
              x
              
                C
                ⁢
                
                  
                
                ⁢
                
                  O
                  2
                
              
            
            /
            
              x
              i
            
          
          
            
              y
              
                C
                ⁢
                
                  
                
                ⁢
                
                  O
                  2
                
              
            
            /
            
              y
              i
            
          
        
      
    
    
      
        (
        8
        )
      
    
  




where x and y refer to the molar composition of the adsorbed phase and the gas phase, respectively.
5—Kinetics of Gas Adsorption:
Kinetic studies of CO2, N2, O2, H2 and CH4 adsorption on SIFSIX-3-Zn were carried out using the Rubotherm gravimetric apparatus operating in dynamic regime (Scheme 51). Initially, SIFSIX-3-Zn was properly evacuated at 298 K. In order to achieve an immediate constancy of pressure (0.5 bar) during kinetics tests and avoid the often noisy uptake during the rapid introduction of the studied gas, an initial baseline was set-up using helium gas at 0.5 bar for single gases and 1 bar for mixture, then the studied single gas or mixture is flushed with a flow of 300 ml/min to avoid any dependence of the kinetics on the mass flow controller. The fractional uptake was calculated by dividing the non-equilibrium uptake at time ti by the equilibrium uptake at equilibrium. Adsorption kinetics analysis involving CO2/N2:10/90 was carried out at 5 bar to compensate for the combination of the low CO2 partial pressure and the large amount of material studied (1 g).
6—X-Ray Diffraction Studies:
Powder X-Ray Diffraction (PXRD):
PXRD patterns were recorded at room temperature on a Bruker D8 ADVANCE diffractometer at 20 kV, 5 mA for Cu-Kα (λ=1.54056 Å), with a scan speed of 1 s/step and a step size of 0.02° in 2θ (total scan duration=30 min.).
Single-Crystal X-Ray Diffraction:
Single crystal x-ray diffraction data for SIFSIX-2-Cu were collected using a Bruker-AXS SMART-APEXII CCD diffractometer equipped with CuKα radiation (λ=1.54178 Å). Diffraction data for SIFSIX-2-Cu-i were collected using synchrotron radiation (λ=0.49594 Å) at the Advanced Photon Source, Chicago, Ill.
Indexing was performed using APEX22 (difference vectors method). Data integration and reduction were performed using SaintPlus 6.013. Absorption correction was performed by the multi-scan method implemented in SADABS4. Space groups were determined using XPREP implemented in APEX2. The structure was solved using SHELXS-97 (direct methods) and refined using SHELXL-97 (full-matrix least-squares on F2) contained in APEX2 and WinGX v1.70.015-8 programs packages. Hydrogen atoms were placed in geometrically calculated positions and included in the refinement process using a riding model with isotropic thermal parameters: Uiso(H)=1.2Ueq(—CH). For SIFSIX-2-Cu the contribution of heavily disordered solvent molecules was treated as diffuse using the Squeeze procedure implemented in Platon9,10. In the structure of SIFSIX-2-Cu-i a methanol molecule is disordered over two positions. The amount of methanol in the crystal was established through occupancy refinement of the oxygen atom. The hydrogen atom of the hydroxyl group was placed in a geometrically calculated position and refined using an H . . . F distance restraint. This distance was chosen based on a search of the Cambridge Structural Database11. For both structures the disordered SiF6 was refined using the SADI geometry restraint. Crystal data and refinement conditions are shown in Tables 1 and 2 for the Supplemental section.
7—Effect of Moisture Upon Gas Adsorption:
The impact of water vapor on CO2 capacity and selectivity was evaluated in both SIFSIX-2-Cu-i and SIFSIX-3-Zn. CO2 cyclic adsorption studies were performed at humidity levels similar to those in real applications, i.e. 74% RH. Results are summarized below:

    
    
        Water vapor adsorption isotherms for SIFSIX-2-Cu-i and SIFSIX-3-Zn collected under pure N2 atmosphere reveal type I behavior with water uptakes of 20 wt % and 11 wt %, respectively at 74% RH.
        Water sorption affinity/capacity was reduced in the presence of CO2 gas mixtures as revealed by breakthrough experiments at 74% RH for both CO2/H2:30/70 and CO2/N2:10/90 mixtures (1.2-1.5 wt % for SIFSIX-2-Cu-i and SIFSIX-3-Zn). Each material, particularly SIFSIX-3-Zn, exhibits remarkably selective CO2adsorption in the presence of water. (FIGS. 21a, 21b, 22a and 22b).
        Interestingly, the presence of water in the mixture (e.g. CO2/H2:30/70) has a negligible effect at elevated CO2 concentrations. Breakthrough time for CO2 in the presence of 74% RH is only marginally shorter than under dry conditions, thus CO2 uptake and selectivity in the humid mixture are only slightly reduced (1.61 mmol/g and 191 at 74% RH vs. 1.99 mmol/g and 237 at 0% RH for SIFSIX-2-Cu-i; FIG. 21b).
    
    


Analysis of the effect of adsorption/breakthrough cycling on SIFSIX-3-Zn shows very little alteration of CO2 uptake and selectivity in CO2/H2:30/70 and CO2/N2:10/90 mixtures after multiple adsorption cycles. Additionally, the CO2 breakthrough time was not reduced at 74% RH as compared to the breakthrough time at 0% RH (FIGS. 22(a) and 22(b)). This finding is extremely significant; H2O vapor has a negligible effect on the CO2 capture properties, in contrast to the benchmark zeolite 13X, where extensive drying of the gas stream is required to achieve optimal separations12-14.
In addition, the PXRD pattern of SIFSIX-2-Cu-i at variable degrees of relative humidity (5-95%; FIG. 23) showed that crystallinity was retained when the compound was in contact with H2O in the presence of relevant gas mixtures. Variable temperature powder x-ray diffraction (VT-PXRD) experiments reveal thermal stability up to at least 573 K (FIG. 24).
Notably, SIFSIX-3-Zn exhibits a phase change when exposed to relative humidity higher than 35%, as indicated by PXRD peak shifts and the appearance of additional peaks (FIG. 25). Regeneration of the original material, as verified by the reappearance of the major diffraction peaks, is accomplished by heating SIFSIX-3-Zn under vacuum for several hours at 323-373 K. Reducing the % RH alone did not reverse the phase change (FIG. 26). PXRD analyses of regenerated SIFSIX-3-Znafter cyclic breakthrough tests at 74% RH as well as after high pressure sorption experiments confirm the presence of the original material (FIG. 27). VT-PXRD experiments demonstrate that SIFSIX-3-Zn maintains crystallinity up to 523 K (FIG. 28).
8—SIFSIX-3-Zn Modeling Details:


    Force field parameters required for modeling sorbate-MOF interactions were established, including repulsion and dispersion parameters, atomic partial point charges, and interacting atomic point polarizabilities according to considerations presented previously15-17. Grand Canonical Monte Carlo (GCMC) simulations were performed to model CO2 sorption in SIFSIX-3-Zn at experimentally-considered state points.


GCMC-generated CO2 adsorption isotherms for SIFSIX-3-Zn (FIG. 31) are in good agreement with experimental data. The associated molecular configurations reveal that maximum loading at the temperatures considered occurs at one CO2 molecule per unit cell. FIG. 32 shows the electropositive carbon atoms of CO2 interacting strongly with four negatively charged framework fluorine atoms, directing the carbon atoms along the channels parallel to the SIFSIX-3-Zn pillars, consistent with steric constraints.
The simulated Qstvalues are in excellent agreement with experiment, showing a relatively constant Qst of ca. 45 kJ/mol for loadings of up to one CO2 molecule per unit cell (FIG. 33). This is consistent with saturation of the favored sorption sites. The polarizable CO2 model used in this work was developed using a previously described procedure18,19. To verify the accuracy of the model in the bulk environment, an isothermal pressure-density plot was produced at 298.15 K using Grand canonical Monte Carlo (GCMC) methods and the results were compared to the corresponding experimental data20. The isotherm for the model was found to be in excellent agreement with experimental data for the considered pressure range to within joint uncertainties (FIG. 34).
Tables for the Supplemental Section







TABLE 1







Crystal data and structure refinement for SIFSIX-2-Cu








Identification code
SIFSIX-2-Cu, [Cu(dpa)2(SiF6)]n





Empirical formula
C24H16CuF6N4Si


Formula weight
566.04


Temperature
100(2) K


Wavelength
1.54178 Å


Crystal system, space group
Tetragonal, P4/mmm


Unit cell dimensions
a = 13.6316(14) Å α = 90°



b = 13.6316(14) Å β = 90°



c = 7.9680(10) Å γ = 90°


Volume
1480.6(3) Å3


Z, Calculated density
1, 0.635 g/cm3


Absorption coefficient
0.965 mm−1


F(000)
285


Crystal size
0.10 × 0.05 × 0.05 mm


Theta range for data
3.24 to 65.87°


collection



Limiting indices (h, k, l)
(−11/15, −12/15, −9/9)


Reflections collected/
6428/803 (Rint = 0.1021)


unique



Completeness to theta = 
99.10%


65.87°



Absorption correction
Semi-empirical from equivalents


Max. and min. transmission
0.9533 and 0.9097


Refinement method
Full-matrix least-squares on F2


Data/restraints/
803/1/50


parameters



Goodness-of-fit on F2
1.054


Final R indices [I > 2σ(I)]
R1 = 0.0444, wR2 = 0.1013


R indices (all data)
R1 = 0.0515, wR2 = 0.1046


Largest diff. peak and hole
0.654 and −0.366 e/Å−3
















TABLE 2







Crystal data and structure refinement for SIFSIX-2-Cu-i









SIFSIX-2-Cu-i,


Identification code
{[Cu(dpa)2(SiF6)]n•2.5CH3OH}





Empirical formula
C26.50H26CuF6N4O2.50Si


Formula weight
646.14


Temperature
100(2) K


Wavelength
0.49594 Å


Crystal system, space group
Tetragonal, I4/mmm


Unit cell dimensions
a = 13.6490(11) Å α = 90°



b = 13.6490(11) Å β = 90°



c = 8.0920(6) Å γ = 90°


Volume
1507.5(2) Å3


Z, Calculated density
2, 1.423 g/cm3


Absorption coefficient
0.282 mm−1


F(000)
660


Crystal size
0.02 × 0.01 × 0.01 mm


Theta range for data
2.04 to 19.68°


collection



Limiting indices (h, k, l)
(−18/18, −16/18, −8/9)


Reflections collected/
11521/535 (Rint = 0.0444)


unique



Completeness to theta =
98.40%


17.39°



Absorption correction
Semi-empirical from equivalents


Max. and min. transmission
0.9972 and 0.9944


Refinement method
Full-matrix least-squares on F2


Data/restraints/
535/2/58


parameters



Goodness-of-fit on F2
1.012


Final R indices [I > 2σ(I)]
R1 = 0.0455, wR2 = 0.1432


R indices (all data)
R1 = 0.0488, wR2 = 0.1456


Largest diff. peak and hole
0.379 and −0.517 e/Å−3
















TABLE 3







Comparison of experimental and theoretical micropore


volumes (cm3/g) of SIFSIX-2-Cu and SIFSIX-2-Cu-i.











MOM
Vcalca
Vexpb






SIFSIX-2-Cu
1.10
1.15



SIFSIX-2-Cu-i
0.25
0.26





acalculated by Platon9,10


bexperimental value determined by t-plot method













TABLE 4







Force field parameters for the polarizable CO2


model used in the molecular simulations in this work.













Distance






Atomic Site
(Å)a
σ (Å)
ε (K)
q (e−)
α° (Å3)















C
0.000
3.30366
19.61757
0.77134
1.2281


O
1.162
0.00000
0.00000
−0.38567
0.7395


OAb
1.208
2.99429
46.47457
0.00000
0.0000





arefers to the distance from the molecular centre-of-mass.


brefers to the off-atom positions.






References, each of which is incorporated herein by reference

    1. Coe, B. J. et al. Syntheses, spectroscopic and molecular quadratic nonlinear optical properties of dipolar ruthenium(II) complexes of the ligand 1,2-phenylenebis(dimethylarsine). Dalton Trans., 2935-2942 (2004).
    2. Bruker. APEX2. Bruker AXS Inc., Madison, Wis., USA (2010).
    3. Bruker. SAINT. Data reduction software. Bruker AXS Inc., Madison, Wis., USA (2009).
    4. Sheldrick, G. M. SADABS. Program for empirical absorption correction. University of Gottingen, Germany (2008).
    5. Farrugia L. J. Appl. Cryst., 32, 837-838 (1999).
    6. Sheldrick, G. M. SHELXL-97. Program for the refinement of crystal structure (1997).
    7. Sheldrick, G. M. Acta Cryst., A46, 467-473 (1990).
    8. Sheldrick, G. M. Acta Cryst., A64, 112-122 (2008).
    9. Spek, T. L. Acta Cryst., A46, 194-201 (1990).
    10. Spek, T. L. Acta Cryst., A46, c34 (1990).
    11. F. H. Allen. Acta Cryst., B58, 380-388 (2002).
    12. F. Brandani, D. Ruthven. The effect of water on the adsorption of CO2 and C3H8 on Type X zeolites. Ind. Eng. Chem. Res., 43, 8339-834 (2004).
    13. D. Bonenfant, M. Kharoune, P. Niquette, M. Mimeault, R. Hausler, R. Advances in principal factors influencing carbon dioxide adsorption on zeolites. Sci. Technol. Adv. Mater. 9, 013001-013007 (2008).
    14. R. Serna-Guerrero, Y. Belmabkhout, A. Sayari, Further investigations of CO2 capture using triamine-grafted pore-expanded mesoporous silica. Chem. Eng. J. 158, 513-519 (2010).
    15. Belof, J. L., Stern, A. C., Eddaoudi, M. & Space, B. On the mechanism of hydrogen storage in a metal-organic framework material. J. Am. Chem. Soc. 129, 15202-15210 (2007).
    16. Stern, A. C.; Belof, J. L.; Eddaoudi, M.; Space, B. Understanding hydrogen sorption in a polar metal-organic framework with constricted channels. J. Chem. Phys. 136, 034705 (2012).
    17. Forrest, K. A.; Pham, T.; McLaughlin, K.; Belof, J. L.; Stern, A. C.; Zaworotko, M. J.; Space, B. Simulation of the mechanism of gas sorption in a metal-organic framework with open metal sites: Molecular hydrogen in PCN-61. J. Phys. Chem. C. 116 (29), 15538-15549 (2012).
    18. Belof, J. L., Stern, A. C. & Space, B. An accurate and transferable intermolecular diatomic hydrogen potential for condensed phase simulation. J. Chem Theory Comput. 4, 1332-1337 (2008).
    19. McLaughlin, K., Cioce, C. R., Belof, J. L. & Space, B. A molecular H2 potential for heterogeneous simulations including polarization and many-body van der Waals interactions. J. Chem. Phys. 136, 194302 (2012).
    20. Angus, S., Armstrong, B. & de Reuck, K. M. International Thermodynamic Tables of the Fluid State: Carbon Dioxide. Vol. 3 68-76 (Pergamon Press, 1976).
    21. Merel, J., Clausse, M. &Meunier, F. Experimental investigation on CO2 post-combustion capture by indirect thermal swing adsorption using 13X and 5A zeolites. Ind. Eng. Chem. Res. 47, 209-215 (2008).


In regard to the discussion herein including the Examples above and the claims, it should be noted that ratios, concentrations, amounts, and other numerical data may be expressed herein in a range format. It is to be understood that such a range format is used for convenience and brevity, and thus, should be interpreted in a flexible manner to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. To illustrate, a concentration range of “about 0.1% to about 5%” should be interpreted to include not only the explicitly recited concentration of about 0.1 wt % to about 5 wt %, but also include individual concentrations (e.g., 1%, 2%, 3%, and 4%) and the sub-ranges (e.g., 0.5%, 1.1%, 2.2%, 3.3%, and 4.4%) within the indicated range. In an embodiment, the term “about” can include traditional rounding according to measurement techniques and the units of the numerical value. In addition, the phrase “about ‘x’ to ‘y’” includes “about ‘x’ to about ‘y’”.
Many variations and modifications may be made to the above-described embodiments. All such modifications and variations are intended to be included herein within the scope of this disclosure and protected by the following claims.

## Claims

1. A method of capturing CO2 in a gas, comprising:
exposing the gas to a multicomponent metal-organic material (MOM) that has a greater relative affinity for CO2 over a water vapor, wherein the MOM includes at least one of an inorganic linker or an inorganic pillar, wherein the gas includes CO2 and water vapor; and
capturing the CO2 in the MOM.

2. The method of claim 1, wherein the gas includes at least one of the following gases: N2, H2, and CH4, wherein the MOM has a greater relative affinity for CO2 over each one of N2, H2, and CH4.

3. The method of claim 1, wherein the MOM is selected from the group consisting of: [Cu(4,4′-dipyridylacetylene)2(SiF6)]n, where n is 1 to 100,000,000; a pair of interpenetrated nets of [Cu(4,4′-dipyridylacetylene)2(SiF6)]n; and [Zn(pyr)2(SiF6)]n, wherein n is 1 to 100,000,000.

4. The method of claim 1, wherein the MOM has a primitive cubic topology.

5. A system for capturing CO2 in a gas, comprising:
a first structure including a multidimensional metal-organic material (MOM) having a primitive cubic topology, wherein the MOM includes at least one of an inorganic linker or an inorganic pillar, wherein the gas includes CO2 and a water vapor, wherein the MOM has a greater relative affinity for CO2 over the water vapor; and
a second structure for introducing the gas to the first structure, wherein CO2 is removed from the gas after the exposure to the MOM to form a modified gas, wherein the second structure flows the modified gas away from the first structure.

6. The system of claim 5, wherein the gas includes at least one of the following gases: N2, H2, and CH4, wherein the MOM has a greater relative affinity for CO2 over each one of N2, H2, and CH4.

7. A method of separating components in a gas, comprising:
exposing a gas including a first component and a second component to a multidimensional metal-organic material (MOM), wherein the MOM has a greater relative affinity for the first component over a second component, wherein the MOM includes at least one of an inorganic linker or an inorganic pillar, wherein the MOM has a greater relative affinity for CO2 over a water vapor, wherein the first component is CO2 and the second component is selected from the group consisting of N2, H2, or CH4; and
capturing the first component in the MOM.

8. The method of claim 7, wherein the MOM has a greater relative affinity for the first component over water vapor present in the gas.

9. The method of claim 8, wherein the first component is CO2 and the second component is N2.

10. The method of claim 8, wherein the first component is CO2 and the second component is H2.

11. The method of claim 8, wherein the first component is CO2 and the second component is CH4.