Poly(ethylene oxide)-Based Copolymer-IL Composite Membranes for CO2 Separation

Poly(ethylene oxide) (PEO)-based copolymers are at the forefront of advanced membrane materials for selective CO2 separation. In this work, free-standing composite membranes were prepared by blending imidazolium-based ionic liquids (ILs) having different structural characteristics with a PEO-based copolymer previously developed by our group, targeting CO2 permeability improvement and effective CO2/gas separation. The effect of IL loading (30 and 40 wt%), alkyl chain length of the imidazolium cation (ethyl- and hexyl- chain) and the nature of the anion (TFSI-, C(CN)3-) on physicochemical and gas transport properties were studied. Among all composite membranes, PEO-based copolymer with 40 wt% IL3-[HMIM][TFSI] containing the longer alkyl chain of the cation and TFSI- as the anion exhibited the highest CO2 permeability of 46.1 Barrer and ideal CO2/H2 and CO2/CH4 selectivities of 5.6 and 39.0, respectively, at 30 °C. In addition, almost all composite membranes surpassed the upper bound limit for CO2/H2 separation. The above membrane showed the highest water vapor permeability value of 50,000 Barrer under both wet and dry conditions and a corresponding H2O/CO2 ideal selectivity value of 1080; values that are comparable with those reported for other highly water-selective PEO-based polymers. These results suggest the potential application of this membrane in hydrogen purification and dehydration of CO2 gas streams.


Introduction
The increase of carbon dioxide (CO 2 ) concentration in the atmosphere due to anthropogenic activities such as burning of fossil fuels (i.e., coal, oil and natural gas), deforestation and wildfires is the main cause of global warming and climate change [1]. Carbon capture and storage (CCS) is an approach for reducing CO 2 emissions by removing CO 2 from large industrial and power plants, followed by its compression, transport and permanent storage [2]. Removal of CO 2 from hydrogen streams produced by the steam reforming process and water gas shift reaction can also be viewed in a similar context. CO 2 separation using polymeric membranes is a promising technology and has many advantages over other methods, namely absorption, pressure swing adsorption and cryogenic distillation [3]. The advantages include low energy consumption, simple installation and scale-up and eco-friendly characteristics [4,5].
Copolymer and polymeric ionic liquid (PIL)-based membranes containing poly(ethylene oxide) (PEO) units, such as Pebax ® (poly(amide-b-ethylene oxide)), Polyactive TM (PEO 75 PBT 25 ), PEGMA-950 2 and PIL 750 -MeSO 4 , have shown improved CO 2 permeation properties with increasing PEO weight content owing to the higher contribution of polar ethylene oxide (EO) units in the system, which interact favorably with CO 2 [6][7][8][9]. Considering the high CO 2 affinity of PEO groups due to the quadrupole-dipole intermolecular forces between the ether oxygen of PEO (C-O-C) and CO 2 molecules, PEO-based membranes exhibit presence of polar pyridine moieties along with sulfone groups in the polyether backbone enables the formation of hydrogen bonds with water, thereby promoting water vapor permeability towards water-selective membranes.
In this study, three different imidazolium-based ionic liquids containing alkyl chains with varying length and counter anions bis(trifluoromethanesulfonyl)imide ([TFSI] − ) or tricyanomethanide ([C(CN 3 )] -) were incorporated into an aromatic polyether bearing side PEO units (2, ) to yield free-standing, soft composite membranes. The effect of IL nature and loading on morphological, thermal and gas transport properties of the prepared 2,6Py-PEO 350 /IL composite membranes were studied. The water vapor transport properties were also evaluated.

IL Preparation
For the preparation of 1-ethyl-3-methylimidazolium bis(trifluoromethane)sulfonamide ([EMIM][TFSI]), 1 g (6.82 mmol) of [EMIM][Cl] was dissolved in 6 mL of acetonitrile, and a solution of LiTFSI (2.34 g, 8.184 mmol) in 6 mL of acetonitrile was also prepared. Then, the LiTFSI solution was added dropwise to the IL solution at room temperature and left under stirring for 2 days to achieve maximum yield of anion exchange. The mixture was filtered and washed with acetonitrile and methanol for the removal of the excess LiTFSI salt. Finally, the obtained IL was recrystallized in dichloromethane for further purification.
Membranes 2023, 13, x FOR PEER REVIEW 3 of 18 liquids containing CO2-philic anions were chosen to be incorporated into the polymer matrix, owing to their high CO2 solubility, as already reported [16,18]. In addition, it should be stressed that the presence of polar pyridine moieties along with sulfone groups in the polyether backbone enables the formation of hydrogen bonds with water, thereby promoting water vapor permeability towards water-selective membranes. In this study, three different imidazolium-based ionic liquids containing alkyl chains with varying length and counter anions bis(trifluoromethanesulfonyl)imide ([TFSI] − ) or tricyanomethanide ([C(CN3)] -) were incorporated into an aromatic polyether bearing side PEO units (2,6Py-PEO350) to yield free-standing, soft composite membranes. The effect of IL nature and loading on morphological, thermal and gas transport properties of the prepared 2,6Py-PEO350/IL composite membranes were studied. The water vapor transport properties were also evaluated.

IL Preparation
For the preparation of 1-ethyl-3-methylimidazolium bis(trifluoromethane)sulfonamide ([EMIM][TFSI]), 1 g (6.82 mmol) of [EMIM][Cl] was dissolved in 6 mL of acetonitrile, and a solution of LiTFSI (2.34 g, 8.184 mmol) in 6 mL of acetonitrile was also prepared. Then, the LiTFSI solution was added dropwise to the IL solution at room temperature and left under stirring for 2 days to achieve maximum yield of anion exchange. The mixture was filtered and washed with acetonitrile and methanol for the removal of the excess LiTFSI salt. Finally, the obtained IL was recrystallized in dichloromethane for further purification.

Membrane Preparation
All composite and precursor membranes were prepared using the solution-casting method. First, the polymer solution was prepared by dissolving 200 mg of 2,6Py-PEO350 Scheme 1. The precursor copolymer 2,6Py-PEO 350 with composition x = 60 and y = 40.

Membrane Preparation
All composite and precursor membranes were prepared using the solution-casting method. First, the polymer solution was prepared by dissolving 200 mg of 2,6Py-PEO 350 polymer in DMAc (5 wt%

Membrane Characterization
ATR spectra of all membranes were collected from 4000 to 400 cm −1 with a resolution of 4 cm −1 using a platinum ATR Bruker spectrometer. Thermogravimetric analysis (TGA) was performed on a Labys TG (Setaram Instrumentation, Caluire-et-Cuire, France) under N2 flow from 25 to 800 °C with a heating rate of 10 °C min −1 . Differential scanning calorimetry (DSC) was conducted on a Perkin Elmer DSC Q100 instrument (Waltham, MA, USA) under N2 flow, in the temperature range from −100 °C to 200 °C and with a heating rate of 10 °C min −1 . Two heating cycles were performed, and the glass transition temperature was derived from the second cycle. Scanning electron microscopy (SEM) was conducted using a LEO Supra 35VP microscope (Zeiss, Oberkochen, Germany). The crosssections of the membranes were prepared after fracturing in liquid N2.

Single Gas and Gas/Water Vapor Permeation Properties
Single gas permeation properties of precursor 2,6Py-PEO350 and composite membranes were studied at 30 °C using the Wicke-Kallenbach method. The experimental procedure and the description of the permeation cell were previously reported [33]. The addition of 3% H2O in each single gas at the retentate side was only studied for the 2,6Py-PEO350-40IL3 composite membrane, which showed the best single gas permeation prop-Scheme 2. Chemical structures of the ionic liquids used to prepare polymer-IL composite membranes.

Membrane Characterization
ATR spectra of all membranes were collected from 4000 to 400 cm −1 with a resolution of 4 cm −1 using a platinum ATR Bruker spectrometer. Thermogravimetric analysis (TGA) was performed on a Labys TG (Setaram Instrumentation, Caluire-et-Cuire, France) under N 2 flow from 25 to 800 • C with a heating rate of 10 • C min −1 . Differential scanning calorimetry (DSC) was conducted on a Perkin Elmer DSC Q100 instrument (Waltham, MA, USA) under N 2 flow, in the temperature range from −100 • C to 200 • C and with a heating rate of 10 • C min −1 . Two heating cycles were performed, and the glass transition temperature was derived from the second cycle. Scanning electron microscopy (SEM) was conducted using a LEO Supra 35VP microscope (Zeiss, Oberkochen, Germany). The cross-sections of the membranes were prepared after fracturing in liquid N 2 .

Single Gas and Gas/Water Vapor Permeation Properties
Single gas permeation properties of precursor 2,6Py-PEO 350 and composite membranes were studied at 30 • C using the Wicke-Kallenbach method. The experimental procedure and the description of the permeation cell were previously reported [33]. The addition of 3% H 2 O in each single gas at the retentate side was only studied for the 2,6Py-PEO 350 -40IL3 composite membrane, which showed the best single gas permeation properties. While He flow rate of 20 cm 3 min −1 was employed in the permeate side for measurements under dry conditions, He flow rate of 100 cm 3 min −1 was used for wet conditions. The gas permeability (P) was calculated according to the equation: where A is the effective membrane area, p r and p p are the retentate and permeate side partial pressures of the measured gas, respectively, F is the volume fraction of the measured gas present in helium flow, l is the membrane thickness and ϕ v,tot is the volumetric flow rate of helium at the permeate side. Selectivity (α A/B ) was calculated as the ratio of the permeabilities P A and P B of the gases A and B, respectively, using the following equation:

Preparation and Characterization of Polymer-IL Composite Membranes
Mechanically robust, amorphous, soft PEO-based membranes with high PEO contents based on aromatic polyether copolymers bearing main chain 2,6-substituted pyridine segments and short side chain PEO groups (2,6Py-PEO 350 ) have recently been prepared and investigated as CO 2 and water-selective membranes by our group [8]. The high content of CO 2 -philic PEO groups induces severe plasticization of the rigid polymer backbone, as reflected by the shifting of T g values to lower temperatures (close to room temperature), thereby resulting in increased chain mobility and flexibility, which in turn leads to increased gas/vapor diffusion. In addition, it has been proven that the incorporation of ionic liquids into the polymer matrix can further improve CO 2 permeability based on their ionic character. For this reason, 2,6Py-PEO 350 copolymer containing 39 wt% PEO was blended with ionic liquids (30 and 40 wt% contents) to prepare composite membranes aiming at CO 2 permeability and separation performance enhancement. In this case, imidazolium-based

ILs including IL1-[EMIM][TFSI], IL2-[EMIM][C(CN) 3 ] and IL3-[HMIM]
[TFSI] were chosen, owing to their high CO 2 solubility [16,18]. All the fabricated composite membranes were flexible, self-standing and soft, as illustrated in Figure 1. It should be noticed that the fabrication of free-standing films with IL loading higher than 40 wt% was not possible because of the instability of the resulting membranes. erties. While He flow rate of 20 cm 3 min −1 was employed in the permeate side for measurements under dry conditions, He flow rate of 100 cm 3 min −1 was used for wet conditions. The gas permeability (P) was calculated according to the equation: where A is the effective membrane area, pr and pp are the retentate and permeate side partial pressures of the measured gas, respectively, F is the volume fraction of the measured gas present in helium flow, l is the membrane thickness and φv,tot is the volumetric flow rate of helium at the permeate side.
Selectivity (αA/B) was calculated as the ratio of the permeabilities PA and PB of the gases A and B, respectively, using the following equation:

Preparation and Characterization of Polymer-IL Composite Membranes
Mechanically robust, amorphous, soft PEO-based membranes with high PEO contents based on aromatic polyether copolymers bearing main chain 2,6-substituted pyridine segments and short side chain PEO groups (2,6Py-PEO350) have recently been prepared and investigated as CO2 and water-selective membranes by our group [8]. The high content of CO2-philic PEO groups induces severe plasticization of the rigid polymer backbone, as reflected by the shifting of Tg values to lower temperatures (close to room temperature), thereby resulting in increased chain mobility and flexibility, which in turn leads to increased gas/vapor diffusion. In addition, it has been proven that the incorporation of ionic liquids into the polymer matrix can further improve CO2 permeability based on their ionic character. For this reason, 2,6Py-PEO350 copolymer containing 39 wt% PEO was blended with ionic liquids (30 and 40 wt% contents) to prepare composite membranes aiming at CO2 permeability and separation performance enhancement. In this case, imid-

azolium-based ILs including IL1-[EMIM][TFSI], IL2-[EMIM][C(CN)3] and IL3-[HMIM]
[TFSI] were chosen, owing to their high CO2 solubility [16,18]. All the fabricated composite membranes were flexible, self-standing and soft, as illustrated in Figure 1. It should be noticed that the fabrication of free-standing films with IL loading higher than 40 wt% was not possible because of the instability of the resulting membranes. As illustrated in Figure 2, the precursor copolymer 2,6Py-PEO350 membrane along with the polymer-IL composite membranes were studied by ATR-FTIR spectroscopy. Regarding the precursor spectrum, the peak signal at 2868 cm −1 is assigned to methylene group vibrations of the PEO units [8,34]. In addition, the doublet peak at 1487 and 1471 cm −1 and the peak signal at 1583 cm −1 correspond to the C=C/C=N vibrations of the pyridine ring [8,35]. Considering that all ILs used in this work for the preparation of polymer- As illustrated in Figure 2, the precursor copolymer 2,6Py-PEO 350 membrane along with the polymer-IL composite membranes were studied by ATR-FTIR spectroscopy. Regarding the precursor spectrum, the peak signal at 2868 cm −1 is assigned to methylene group vibrations of the PEO units [8,34]. In addition, the doublet peak at 1487 and 1471 cm −1 and the peak signal at 1583 cm −1 correspond to the C=C/C=N vibrations of the pyridine ring [8,35]. Considering that all ILs used in this work for the preparation of polymer-IL composite membranes contain a common imidazolium cation, the characteristic peak at 1574 cm −1 assigned to the imidazolium ring in plane symmetric/asymmetric stretch and -CH 2 (N)/-CH 3 (N)CN could not be observed in all composite membrane spectra due to overlapping with the peak at 1583 cm −1 . However, after the addition of ILs containing a TFSIanion, a new peak at 1350 cm −1 appears that can be attributed to the asymmetric stretching of the SO 2 group [9]. The symmetric bending vibrations of the same group are located at 616 cm −1 and 604 cm −1 . The peak located at 1053 cm −1 is assigned to the asymmetric stretching band of the S-N-S group, and its bending vibrations can be identified as very weak peaks at 650 cm −1 and 612 cm −1 . The bands at 789 cm −1 and 509 cm −1 are also attributed to asymmetric bending of the CF 3 group and the C-S bond of the TFSIanion, respectively. After addition of IL containing a C(CN) 3 anion, a new strong peak arose at 2158 cm −1 , attributed to the stretching vibration of the -CN group [9,36]. No shifts were observed in the ATR-IR spectra of 2,6Py-PEO 350 -IL membranes compared to those of neat 2,6Py-PEO 350 copolymers.
IL composite membranes contain a common imidazolium cation, the characteristic peak at 1574 cm −1 assigned to the imidazolium ring in plane symmetric/asymmetric stretch and -CH2(N)/-CH3(N)CN could not be observed in all composite membrane spectra due to overlapping with the peak at 1583 cm −1 . However, after the addition of ILs containing a TFSIanion, a new peak at 1350 cm −1 appears that can be attributed to the asymmetric stretching of the SO2 group [9]. The symmetric bending vibrations of the same group are located at 616 cm −1 and 604 cm −1 . The peak located at 1053 cm −1 is assigned to the asymmetric stretching band of the S-N-S group, and its bending vibrations can be identified as very weak peaks at 650 cm −1 and 612 cm −1 . The bands at 789 cm −1 and 509 cm −1 are also attributed to asymmetric bending of the CF3 group and the C-S bond of the TFSIanion, respectively. After addition of IL containing a C(CN)3 -anion, a new strong peak arose at 2158 cm −1 , attributed to the stretching vibration of the -CN group [9,36]. No shifts were observed in the ATR-IR spectra of 2,6Py-PEO350-IL membranes compared to those of neat 2,6Py-PEO350 copolymers. Thermogravimetric analysis (TGA) was used to investigate the thermal stability of polymer-IL composite membranes. The TGA curves of precursor polymer and composite membranes containing 30 wt% IL are given in Figure 3. The precursor shows two main degradation steps, where the first step is observed at around 330 °C, assigned to the loss of PEO side groups [8]  , an initial weight loss up to 210 °C (1.5 and 3.5 wt%, respectively) was observed, attributed to DMAc residual solvent. For the latter, a second small weight loss at around 320 °C was evident, attributed to the evaporation of the corresponding IL3 [37]. All composite membranes show two main weight loss steps. The first starts at around 305-330 °C, associated with the degradation of side PEO groups, and the second one, at about 400-430 °C, is due to polymer backbone and ionic liquid degradation simultaneously. Indeed, for example, the reported degradation temperature of IL1 is 393 °C, which is in good agreement with our results [38]. Comparison of the TGA curves of the composite membranes containing imidazolium ILs with different alkyl chain length reveals that thermal degradation of the composite membrane with an imidazolium cation with a Thermogravimetric analysis (TGA) was used to investigate the thermal stability of polymer-IL composite membranes. The TGA curves of precursor polymer and composite membranes containing 30 wt% IL are given in Figure 3. The precursor shows two main degradation steps, where the first step is observed at around 330 • C, assigned to the loss of PEO side groups [8] and the second one is at 430 • C, corresponding to the polymer backbone degradation. Regarding composite membranes containing IL1- [EMIM][TFSI] and IL3-[HMIM][TFSI], an initial weight loss up to 210 • C (1.5 and 3.5 wt%, respectively) was observed, attributed to DMAc residual solvent. For the latter, a second small weight loss at around 320 • C was evident, attributed to the evaporation of the corresponding IL3 [37]. All composite membranes show two main weight loss steps. The first starts at around 305-330 • C, associated with the degradation of side PEO groups, and the second one, at about 400-430 • C, is due to polymer backbone and ionic liquid degradation simultaneously. Indeed, for example, the reported degradation temperature of IL1 is 393 • C, which is in good agreement with our results [38]. Comparison of the TGA curves of the composite membranes containing imidazolium ILs with different alkyl chain length reveals that thermal degradation of the composite membrane with an imidazolium cation with a shorter alkyl chain length (IL1) starts at a higher temperature (T d~3 30 • C) than the degradation of the corresponding with the longer alkyl chain (T d~3 20 • C). This result may be explained by the stronger electrostatic interactions between the precursor copolymer and ionic liquid containing imidazolium cations with a shorter alkyl chain length, thus delaying the composite decomposition. In addition, the effect of anion nature on thermal stability was also investigated. Among composite membranes containing 30 wt% IL, the one with the TFSIanion shows higher thermal stability than the corresponding with the C(CN) 3 anion (the decomposition for the former starts at 330 • C, and for the latter at 305 • C). This is in agreement with the degradation temperatures determined for neat ILs [38]. The thermal stability of all prepared membranes incorporated with ionic liquid was found to be sufficient at temperatures up to~300 • C, suggesting the suitability of these membranes for gas separation applications. radation of the corresponding with the longer alkyl chain (Td ~ 320 °C). This result may be explained by the stronger electrostatic interactions between the precursor copolymer and ionic liquid containing imidazolium cations with a shorter alkyl chain length, thus delaying the composite decomposition. In addition, the effect of anion nature on thermal stability was also investigated. Among composite membranes containing 30 wt% IL, the one with the TFSIanion shows higher thermal stability than the corresponding with the C(CN)3 -anion (the decomposition for the former starts at 330 °C, and for the latter at 305 °C). This is in agreement with the degradation temperatures determined for neat ILs [38]. The thermal stability of all prepared membranes incorporated with ionic liquid was found to be sufficient at temperatures up to ~300 °C, suggesting the suitability of these membranes for gas separation applications. Differential scanning calorimetry (DSC) was used to determine the glass transition temperatures of the polymer-IL composite membranes, as depicted in Figure 4. Generally, all composite membranes display lower glass transition temperatures (Tgs) compared to the neat copolymer, with a more pronounced reduction for higher IL contents. For instance, the composite membrane containing 30 wt% IL1- [EMIM][TFSI] has a Tg value of 15.4 °C, while an increase in IL1 content (40 wt%) is followed by a further Tg decrease to −7.3 °C. This is due to the plasticization effect, resulting in flexible and soft membrane structures [18] with increased free volume and, consequently, lower Tg, as already reported [35,38]. Regarding the effect of the anion's chemical structure on Tg, the comparison of composite membranes containing the same IL content (40 wt%) but ILs with different counter anions (TFSIand C(CN)3 -), reveals that the Tg of composite membranes containing IL2-[EMIM][C(CN)3] is higher (4 °C) than the corresponding of composite membranes with IL1. This can probably be attributed to the lower molar volume of the C(CN)3anion (123.33 Å 3 ) [39] compared to the TFSIanion (208.3 Å 3 ) [40]. As a consequence, the chain mobility is restricted since the C(CN)3 -anion can be accommodated in the available free interchain space, thus leading to the free volume reduction and, thereby, to Tg increase. The lowest Tg value of −18.3 °C was observed for the composite membrane comprising an imidazolium cation with hexyl groups (IL3) having 40 wt% IL content, while the corresponding one with shorter chain length (ethyl groups) has a Tg value of −7.3 °C. Differential scanning calorimetry (DSC) was used to determine the glass transition temperatures of the polymer-IL composite membranes, as depicted in Figure 4. Generally, all composite membranes display lower glass transition temperatures (T g s) compared to the neat copolymer, with a more pronounced reduction for higher IL contents. For instance, the composite membrane containing 30 wt% IL1- [EMIM][TFSI] has a T g value of 15.4 • C, while an increase in IL1 content (40 wt%) is followed by a further T g decrease to −7.3 • C. This is due to the plasticization effect, resulting in flexible and soft membrane structures [18] with increased free volume and, consequently, lower T g , as already reported [35,38]. Regarding the effect of the anion's chemical structure on T g , the comparison of composite membranes containing the same IL content (40 wt%) but ILs with different counter anions (TFSIand C(CN) 3 -), reveals that the T g of composite membranes containing IL2-[EMIM][C(CN) 3 ] is higher (4 • C) than the corresponding of composite membranes with IL1. This can probably be attributed to the lower molar volume of the C(CN) 3 anion (123.33 Å 3 ) [39] compared to the TFSIanion (208.3 Å 3 ) [40]. As a consequence, the chain mobility is restricted since the C(CN) 3 anion can be accommodated in the available free interchain space, thus leading to the free volume reduction and, thereby, to T g increase. The lowest T g value of −18.3 • C was observed for the composite membrane comprising an imidazolium cation with hexyl groups (IL3) having 40 wt% IL content, while the corresponding one with shorter chain length (ethyl groups) has a T g value of −7.3 • C. The increase of the alkyl chain length of the cation results in free volume and chain mobility increase, thus leading to T g decrease. For all composite membranes, the presence of a single T g indicates the successful incorporation of the three different ILs into the polymer matrix. It should be noted that all composite membranes are in the rubbery state at 30 • C, the temperature used for water vapor and gas permeation experiments in this study.
The increase of the alkyl chain length of the cation results in free volume and chain mobility increase, thus leading to Tg decrease. For all composite membranes, the presence of a single Tg indicates the successful incorporation of the three different ILs into the polymer matrix. It should be noted that all composite membranes are in the rubbery state at 30 °C, the temperature used for water vapor and gas permeation experiments in this study. The membrane morphology plays a vital role in gas separation and purification performance. The cross-sectional SEM micrographs of polymer-IL composite membranes containing 40 wt% of each IL are illustrated in Figure 5. It was revealed that all membranes are dense, smooth and not phase-separated. This suggests that ILs were uniformly distributed into the polymer matrix, leading to non-porous, homogeneous structures. Similar observations were reported for the Pebax ® 1657/(Emim]BF4]) polymer IL pair by Rabiee et al. [18]. The thickness of the membranes ranges from 47 to 165 μm.  The membrane morphology plays a vital role in gas separation and purification performance. The cross-sectional SEM micrographs of polymer-IL composite membranes containing 40 wt% of each IL are illustrated in Figure 5. It was revealed that all membranes are dense, smooth and not phase-separated. This suggests that ILs were uniformly distributed into the polymer matrix, leading to non-porous, homogeneous structures. Similar observations were reported for the Pebax ® 1657/(Emim]BF 4 ]) polymer IL pair by Rabiee et al. [18]. The thickness of the membranes ranges from 47 to 165 µm.

Gas Separation Properties of Polymer-IL Composite Membranes
The gas separation properties of the 2,6Py-PEO350 precursor copolymer and the composite membranes were determined using the Wicke-Kallenbach method at 30 °C. The gas permeability data (CO2, CH4, H2) are shown in Table 1. It was observed that the precursor copolymer exhibits much lower gas permeability than composite membranes con-

Gas Separation Properties of Polymer-IL Composite Membranes
The gas separation properties of the 2,6Py-PEO 350 precursor copolymer and the composite membranes were determined using the Wicke-Kallenbach method at 30 • C. The gas permeability data (CO 2 , CH 4 , H 2 ) are shown in Table 1. It was observed that the precursor copolymer exhibits much lower gas permeability than composite membranes containing the imidazolium-based ILs with TFSI - (IL1 and IL3). Generally, IL molecules plasticize the polymer matrix, leading to improved chain mobility and increased free volume, and consequently to enhanced gas diffusivity and permeability [18,[41][42][43][44]. However, solubility also plays a significant role in permeability according to the solubility-diffusion mechanism for dense membranes [45]. For instance, ILs with TFSIand C(CN) 3 as counter anions are reported to show high CO 2 solubility due to chemical interactions of CO 2 molecules with the anions [46][47][48]. In addition, the higher fractional free volume of ILs compared to polymers facilitates the CO 2 diffusion across composite membranes [38]. In contrast to this, CH 4 and H 2 have no significant interactions with ILs [38], thus very small additional solubility contribution is expected for CH 4 and H 2 in composite membranes, and, therefore, diffusion mainly contributes to CH 4 and H 2 permeability increases. As a result, the permeability increment is more significant for CO 2 instead of H 2 and CH 4 due to the high diffusivity and solubility of CO 2 in a polymer and IL matrix, respectively. For this reason, CO 2 /CH 4 and CO 2 /H 2 ideal selectivities are also increased with the addition of ILs. In contrast, the incorporation of the imidazolium-based IL with C(CN) 3 -(IL2) into the polymer matrix caused a clear reduction of CH 4 and H 2 permeability, while CO 2 permeability was almost not affected. The reduction is more pronounced for H 2 than CH 4 . This phenomenon could be possibly attributed to two reasons. The lower molar volume of the C(CN) 3 counter anion enables IL accommodation in the initial available free interchain spacing, thus restricting chain mobility and resulting in smaller interchain spacing for gas transport. Another reason could be the strong interactions of the IL cation with the C(CN) 3 anion and/or PEO groups of the precursor with IL ionic moieties that can lead to a tighter and more compact structure. As the restriction induced by the strong interactions has a more considerable effect on permeability than plasticization, the CH 4 and H 2 permeabilities were decreased. Table 1. Single gas permeability and CO 2 selectivity over other gases of the precursor polymer and the polymer-IL composite membranes (1 Barrer = 10 −10 cm 3 (STP) cm cm −2 s −1 cm Hg −1 ). The effect of IL content on gas separation properties was studied. The permeability of all gases is significantly increased by increasing the IL loading in the host polymer matrix for all composite membranes. Besides plasticization effect and free volume increase discussed above, the higher intrinsic permeability of ILs may also contribute significantly to the increase of gas permeabilities [46] [38].

Polymer-IL Membranes
Another factor that may influence the gas separation properties is the alkyl chain length in the imidazolium cation. As shown in Table 1, by comparing the CO 2 and CH 4 permeability values of 2,6Py-PEO 350 -40IL3 containing the hexyl chain substituent in the cation with the corresponding membrane having the ethyl chain substituent (IL1), it is evident that the former has 1.9-and 2.5-times higher values, respectively, than the latter. The longer alkyl chains probably enable the better distribution of the IL into the polymer matrix, thus inducing a stronger plasticization and free volume increase, which facilitates gas diffusion and, consequently, gas permeability increase. The same trend was also reported by X. Li et al. [23]. In particular, Pebax ® 1657 composite membranes containing imidazolium ILs having different alkyl chain lengths (ethyl and hexyl groups in the cation) were prepared, and a significant CO 2 permeability increment was observed with increasing alkyl chain length.
Concerning the effect of the IL anion on gas transport, it was observed that composite membranes containing the C(CN) 3 anion (IL2) exhibit significantly lower permeability for all gases than the corresponding membranes with the TFSIanion (with 30 or 40 wt% IL content). This is attributed to the denser polymer chain packing due to strong interactions of IL cation and anion and/or PEO groups with IL ionic moieties, thus contributing to gas diffusion decrease and, thereby, to gas permeability decrease [9]. However, in supported IL membranes containing TFSIand C(CN) 3 anions, the CO 2 permeability appears not to be affected by the type of anion under the same measurement conditions [49]. On the other hand, it would be expected that, due to the high number of cyano groups contained in IL2, CO 2 permeability and solubility should be high [48]. However, this seems not to be the case neither for the prepared composite membranes of this work as evidenced by the gas permeability data, nor for other PEO-based PILs [9].
Pure gas permeabilities of the precursor and the polymer-IL composite membranes follow the order CO 2 (3.30 Å) > H 2 (2.87 Å) > CH 4 (3.80 Å) [50], where CO 2 has higher permeability than H 2 , although the latter has smaller kinetic diameter. Consequently, the precursor and all composite membranes exhibit CO 2 /H 2 "reverse selectivity", in which CO 2 is preferentially transported across the membrane over H 2 . This is mostly characteristic for rubbery polymers or those that can strongly interact with CO 2 molecules such as PEO-based membranes [8]. In specific, these polymers exhibit high CO 2 solubility due to significant interactions of quadrupole CO 2 molecules with polar PEO groups, thus resulting in higher CO 2 permeability. In glassy polymers, the opposite trend is observed, as the diffusion-controlled gas transport dominates leading to the preferential transport of H 2 over CO 2 . The composite membrane with 40 wt% [HMIM][TFSI] (IL3) achieved the highest CO 2 gas permeability value of 46.1 Barrer with corresponding ideal selectivity values of 39 and 5.6 for CO 2 /CH 4 and CO 2 /H 2 pairs, respectively.
Comparison of gas permeability and selectivity of the precursor and the prepared composite membranes for the CO 2 /CH 4 gas pair with a PEO-based polymer and other polymer/IL membranes reported in the literature is shown in Figure 6A. It can be noticed that their separation performance is comparable or even higher than the other membranes investigated. In addition, all prepared composite membranes show improved CO 2 /CH 4 separation performance (selectivity varying in the range of 39-64) compared to the precursor membrane (33), owing to the presence of ILs, which exhibit high CO 2 solubility and permeability. These data lie close but below the 2008 Robeson upper bound line. The composite membrane containing 30 wt% IL3 exhibits the highest CO 2 /CH 4 selectivity (64) among all composite membranes. The significant increase of CO 2 /CH 4 selectivity (almost 2 times higher than the precursor membrane) can be ascribed to the relative permeability increment of CO 2 , which is more pronounced compared to that of CH 4 . While for methane the permeability increase is mostly owed to diffusivity increase, the contribution of both solubility and diffusivity on permeability enhancement for CO 2 is evident. A similar CO 2 /CH 4 selectivity value of 72 for Pebax ® MH 1657 blended with 20 wt% of [C 4 MIM][Gly] was reported [23]. Although with increasing IL content there is no clear trend for CO 2 /CH 4 selectivity, in the case of composite membranes containing IL2, both CO 2 permeability and CO 2 /CH 4 selectivity increased, suggesting that this system does not follow the typical "trade off" behavior between permeability and selectivity. On the contrary, the increase of IL content in composite membranes containing IL3 results in the deterioration of CO 2 /CH 4 separation performance. In addition, the anion's effect on CO 2 /CH 4 selectivity was studied and revealed that by switching from TFSI --(IL3) to C(CN) 3 --containing composite membranes, the selectivity is reduced from 64 to 39, respectively. This is mainly related to the reduction of CO 2 permeability, which is more significant compared to that of CH 4 . A possible explanation is that composite membranes containing the C(CN) 3 counter anion exhibit a tighter polymer chain packing due to strong interchain electrostatic interactions between the IL cation and anion and/or between PEO groups and IL ionic moieties, which hinders gas diffusion and thus leads to permeability decrease. As evidenced in Figure 6B, almost all polymer-IL composite membrane surpassed the upper bound limit for CO2/H2 separation, while precursor polymer 2,6Py-PEO350 lies below this limit. All composite membranes (with 30 wt% IL) showed simultaneously higher CO2 permeability and CO2/H2 selectivity than the neat copolymer. The CO2/H2 As evidenced in Figure 6B, almost all polymer-IL composite membrane surpassed the upper bound limit for CO 2 /H 2 separation, while precursor polymer 2,6Py-PEO 350 lies below this limit. All composite membranes (with 30 wt% IL) showed simultaneously higher CO 2 permeability and CO 2 /H 2 selectivity than the neat copolymer. The CO 2 /H 2 ideal selectivity enhancement can be mainly attributed to the increased CO 2 diffusivity and CO 2 solubility of the ILs. By increasing IL content from 30 to 40 wt%, the CO 2 /H 2 selectivity was further increased. The positive effect of increasing IL content on CO 2 /H 2 selectivity was also reported for Pebax ® 1657/[Emim] [BF 4 ] [18]. The 2,6Py-PEO 350 with 40 wt% [EMIM][TFSI] (IL1) has the best CO 2 /H 2 selectivity value of 6.4 and a CO 2 permeability value of 24.7 Barrer. The separation performance of the composite membranes of this work is comparable with other PEO-based copolymer membranes and polymer/IL composite membranes reported in the literature, despite their lower CO 2 permeability, as depicted in Figure 6B. For instance, Bernardo SO 3 ] and reported that the composite membrane containing 40 wt% IL content exhibited an ideal CO 2 /H 2 selectivity value of 8.5 and a CO 2 permeability value of 150 Barrer [12].
In conclusion, a prospective strategy for enhancing the CO 2 separation properties of polymer-IL composite membranes comprises the successful tailoring of IL types (cation, anion) having high CO 2 solubility combined with a high CO 2 affinity polymer matrix.

Water Vapor Separation Properties of Polymer-IL Composite Membranes
The water vapor permeation properties of the precursor polymer and the 2,6Py-PEO 350 -40IL3 composite membrane with the highest gas permeabilities (CO 2 , CH 4 , H 2 ), were also studied ( Figure 7, Table 2). In specific, the precursor polymer had a water vapor permeability of 8900 Barrer, as the presence of polar pyridine units in the polyether backbone and side hydrophilic PEO groups enables the formation of hydrogen bonds with water, thus promoting water vapor permeability. The addition of 40 wt% [HMIM][TFSI] (IL3) into the polymer matrix had a positive effect on water vapor permeability. In specific, a substantial increase of water vapor permeability by 5.6 times to 50,000 Barrer was observed. The strong plasticization induced by the incorporation of IL3 causes a significant increase of free volume, thus facilitating water vapor diffusion and, consequently, water vapor permeability enhancement. It should be stressed that water vapor permeability is mainly governed by the hydrophilicity and hydrogen bond basicity of the counter anion in PILs, as recently reported by our group [9]. In the case of the 2,6Py-PEO 350 -40IL3 composite membrane, despite the hydrophobic character of [HMIM][TFSI] (IL3) and its weak proton acceptor ability (due to the electron-withdrawing effect of fluorine atoms in TFSI -), the hydrogen bond between water molecules and the TFSIanion do form. However, the water vapor permeability improvement is mainly attributed to the high diffusivity and to a lesser extent to solubility. The H 2 O/CO 2 selectivity of the composite membrane was significantly declined by 50% to 1080 compared to the corresponding one of precursor membrane. To the best of our knowledge, water vapor permeability data of polymer-IL composite membranes are limited, and, consequently, a comparison can be made only with hydrophilic polymers containing PEO groups. As illustrated in Figure 7, the water vapor permeation behavior of the present composite membrane is on par with other PEO-based polymers such as Pebax ® 1074, Polyactive TM and PEO-PBT. These results underline the potential of this composite membrane for dehydration applications.
nificantly declined by 50% to 1080 compared to the corresponding one of precursor membrane. To the best of our knowledge, water vapor permeability data of polymer-IL composite membranes are limited, and, consequently, a comparison can be made only with hydrophilic polymers containing PEO groups. As illustrated in Figure 7, the water vapor permeation behavior of the present composite membrane is on par with other PEO-based polymers such as Pebax ® 1074, Polyactive TM and PEO-PBT. These results underline the potential of this composite membrane for dehydration applications.   Gas permeation properties of the 2,6Py-PEO 350 -40IL3 membrane were also studied under wet conditions. A total of 3% H 2 O was added in the feed flow of each gas at the retentate side to investigate how the presence of water can affect gas permeability and selectivity. The gas permeation properties of 2,6Py-PEO 350 -40IL3 under dry and wet conditions are given in Table 2. It is evident that CO 2 and CH 4 permeability remained unchanged (considering the given errors), while H 2 permeability was slightly increased (11.0 Barrer). As a result, gas selectivities/separation factors (SF) were not noticeably affected, and H 2 O/gas separation factors remained unaltered. On the other hand, Dai et al. [65] used the IL [TETA][tfa] for the preparation of Pebax ® /TSIL blends and reported that the presence of water vapor (high relative humidity) in feed gas enables membrane swelling, which favors gas diffusion. In specific, CO 2 permeability of a composite membrane containing 30 wt% IL changed from around 250 to 567 GPU, denoting the positive role of water vapor on gas transport through membranes. As [TETA][tfa] is a very hydrophilic IL, the membrane is strongly plasticized by water molecules, thus leading to gas diffusion increase. In contrast, in the case of the prepared membrane containing the [HMIM][TFSI], swelling is not favored due to the IL's hydrophobic character. For this reason, the presence of water vapor does not affect the separation properties.

Conclusions
Free-standing PEO-based copolymer-IL composite membranes were successfully prepared via the solution casting method by incorporating up to 40 wt% of three different ILs into the 2,6Py-PEO 350 polymer matrix. The prepared composite membranes are amorphous and rubbery with low T g values, as revealed by DSC. In addition, they are homogeneous, indicative of the good dispersion of the ILs into the polymer matrix and have high thermal stability up to~300 • C, as evidenced by SEM and TGA analysis, respectively. The addition of ILs containing different alkyl chain length in imidazolium and anions (TFSI -, C(CN 3 ) -) into the polymer matrix (30 wt%) caused a significant increase of both CO 2 and CO 2 /H 2 selectivity compared to the neat PEO-based copolymer. The composite membrane with 40 wt% [HMIM][TFSI] (IL3) achieved the highest CO 2 gas permeability value of 46.1 Barrer with corresponding ideal selectivity values of 39 and 5.6 for CO 2 /CH 4 and CO 2 /H 2 pairs, respectively. Almost all polymer-IL composite membranes surpassed the upper bound limit for CO 2 /H 2 separation, while the precursor polymer 2,6Py-PEO 350 lies below this limit. The CO 2 /H 2 ideal selectivity enhancement can be mainly attributed to the increased CO 2 diffusivity and CO 2 solubility of the ILs. Regarding the alkyl chain length in the imidazolium cation, the comparison of the CO 2 and CH 4 permeability values of 2,6Py-PEO 350 -40IL3 containing the hexyl chain substituent in the cation with the corresponding membrane having the ethyl chain substituent (IL1) revealed that longer alkyl chains lead to free volume increase, which facilitates gas diffusion and, consequently, gas permeability increase. The positive effect of increasing IL loading on gas permeabilities was also revealed. Concerning the IL anion's nature effect on gas transport, it was observed that composite membranes containing the C(CN) 3 anion (IL2) exhibit significantly lower permeability for all gases than the corresponding membranes with the TFSIanion (with 30 or 40 wt% IL content), which is attributed to the denser polymer chain packing that hinders gas diffusion and therefore results in reduced permeability. The composite membrane with 40 wt% [HMIM][TFSI] (IL3) also exhibits the highest water vapor permeability value of 50,000 Barrer and a corresponding H 2 O/CO 2 ideal selectivity value of 1080, which are comparable to those reported for other highly water-selective PEO-based polymers. Therefore, it could be a potential candidate for hydrogen purification and dehydration of CO 2 gas streams. Funding: This research was funded by the project "Bioconversion of lignite power plant emissions to fuels and fine chemicals (BIOMEK)" (MIS T1E∆K-00279), which is implemented under the "EPAnEK 2014-2020 Operational Programme", funded by the Operational Programme "Competitiveness, Entrepreneurship and Innovation" (NSRF 2014-2020) and co-financed by Greece and the European Union (European Regional Development Fund).