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Article

Thin Film Mixed Matrix Hollow Fiber Membrane Fabricated by Incorporation of Amine Functionalized Metal-Organic Framework for CO2/N2 Separation

by
Guoqiang Li
1,
Wojciech Kujawski
1,2,*,
Katarzyna Knozowska
1 and
Joanna Kujawa
1
1
Department of Physical Chemistry and Physical Chemistry of Polymers, Faculty of Chemistry, Nicolaus Copernicus University in Toruń, 7 Gagarina Street, 87-100 Toruń, Poland
2
Moscow Engineering Physics Institute, National Research Nuclear University MEPhI, 31 Kashira Hwy, 115409 Moscow, Russia
*
Author to whom correspondence should be addressed.
Materials 2021, 14(12), 3366; https://doi.org/10.3390/ma14123366
Submission received: 17 May 2021 / Revised: 11 June 2021 / Accepted: 15 June 2021 / Published: 17 June 2021
(This article belongs to the Special Issue Polymers, Multifunctional Nanomaterials, and Composites)
Browse Figures
Versions Notes

Abstract

:
Membrane separation technology can used to capture carbon dioxide from flue gas. However, plenty of research has been focused on the flat sheet mixed matrix membrane rather than the mixed matrix thin film hollow fiber membranes. In this work, mixed matrix thin film hollow fiber membranes were fabricated by incorporating amine functionalized UiO-66 nanoparticles into the Pebax® 2533 thin selective layer on the polypropylene (PP) hollow fiber supports via dip-coating process. The attenuated total reflection-Fourier transform infrared (ATR-FTIR), scanning electron microscope (SEM), energy-dispersive X-ray spectroscopy (EDX) mapping analysis, and thermal analysis (TGA-DTA) were used to characterize the synthesized UiO-66-NH2 nanoparticles. The morphology, surface chemistry, and the gas separation performance of the fabricated Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membranes were characterized by using SEM, ATR-FTIR, and gas permeance measurements, respectively. It was found that the surface morphology of the prepared membranes was influenced by the incorporation of UiO-66 nanoparticles. The CO2 permeance increased along with an increase of UiO-66 nanoparticles content in the prepared membranes, while the CO2/N2 ideal gas selectively firstly increased then decreased due to the aggregation of UiO-66 nanoparticles. The Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membranes containing 10 wt% UiO-66 nanoparticles exhibited the CO2 permeance of 26 GPU and CO2/N2 selectivity of 37.

1. Introduction

Global warming resulted from greenhouse gas has created serious consequence for the environment, e.g., melting glaciers. In comparison with other greenhouse gases, CO2 is one of the important contributors to global warming [1]. CO2 emission increases significantly every year due to the rapid development of industry and the more intensive human activities. The flue gas released by power plant due to the usage of fossil fuels is the main source of CO2 emission [2]. Therefore, the separation of CO2 from flue gas mixture to mitigate the CO2 emission plays an important role in the environment protection and the sustainable development of the industry [3]. Membrane separation technology, physical and chemical adsorption, and cryogenic separation have been used in the CO2 capture process [1,4,5].
Membrane separation technology is widely considered as an alternative to the traditional intensively energy-consuming technologies for CO2 separation [6]. Various types of membrane have been used for CO2 capture from flue gas mixture, such as polymeric membranes [7,8], inorganic membranes [9], and mixed matrix membranes (MMMs) [10,11,12].
Pebax® materials are used for MMMs fabrication because of their advantages, e.g., desirable separation performance and high processability [13]. They are good candidates for polymeric membrane matrix for CO2/N2 separation due to their desirable CO2 permeance, high ideal selectivity, and tunability of gas separation properties via the incorporation of nanofillers [14]. Pebax® 2533 shows higher CO2 permeability with desirable CO2/N2 selectivity [15]. Therefore, Pebax® 2533 was chosen as the polymer matrix for the preparation of thin film mixed matrix hollow fiber membranes in this work. Thin film Pebax® 2533/polyetherimide (PEI) composite hollow fiber membranes were fabricated via dip coating method and assembled into a lab-scale hollow fiber module for CO2/N2 separation [13]. In the pure gas permeance test, the prepared membranes exhibited CO2 and N2 permeances equal to 48 and 1.6 GPU, respectively, at 23 °C and 790 kPa, while the CO2 and N2 permeances are 36 and 1.7 GPU, respectively, in the gas mixture permeance test under the same testing conditions. The CO2 permeance from gas mixture test was 12 GPU lower than that from pure gas test. However, the N2 permeance in both cases are practically the same [13].
MMMs containing metal-organic framework (MOF) have been intensively studied to improve the comprehensive gas separation properties of membranes. This is because MOFs possess high surface area, high packing capacity, tunable porosity and pore size, chemical functionality, and enormous varieties, which endows them huge advantages for the incorporation into polymer matrix [16,17,18]. MOFs are more intensively used in MMMs for various gas separation processes than other porous fillers [5].
MOFs such as the zeolitic imidazolate framework (ZIF) [17,18,19], Materials Institute Lavoisier (MIL) [20], and University in Oslo (UiO-66) [21,22] are commonly used for the preparation of MMMs for gas separation. Gao et al. [19] incorporated ZIF-7-NH2, ZIF-7-OH, and ZIF-7-CH3OH into Pebax® 2533 matrix to fabricate MMMs. The CO2 adsorption properties of MMMs was enhanced due to the introduction of functional groups in ZIF-7 framework. All the prepared MMMs showed better CO2/N2 separation performance than the pristine Pebax® membranes. The MMM containing 14 wt% ZIF-7-OH particles exhibited high CO2 permeability equal to 273 Barrer and CO2/N2 selectivity equal to 38, which in comparison to the pristine Pebax® membrane increased by 60 and 145%, respectively. Jameh et al. [23] modified ZIF-8 nanoparticles with ethylenediamine (ED) and incorporated them into Pebax® 1074 matrix to fabricate MMMs for CO2 capture. The authors found that the CO2 adsorption capacity of MMM containing ED modified ZIF-8 was higher than that containing ZIF-8. Consequently, CH4 and CO2 permeabilities of the ZIF-8/Pebax® MMMs are 9.39 and 134 Barrer, respectively, while for the ED-ZIF-8/Pebax® MMMs, the CH4 and CO2 permeabilities were 14.2 and 344 Barrer, respectively. Dai et al. [24] incorporated ZIF-8 into polyetherimide (PEI) matrix to prepare dual layer mixed matrix hollow fiber membranes via dry jet-wet spinning technique. It was found that presence of ZIF-8 increased the CO2 permeance and CO2/N2 ideal selectivity from 13 GPU and 34 to 21 GPU and 39, respectively, in comparison to pure PEI hollow fiber membranes. Etxeberria-Benavides et al. [25] prepared polybenzimidazole (PBI) mixed matrix hollow fiber membranes containing ZIF-8 for H2/CO2 separation. The prepared membranes showed high H2 permeance of 107 GPU at 7 bar and 70 °C in comparison with 65 GPU of pristine PBI hollow fiber membranes. While the H2/CO2 selectivity was constant. For the mixed gas permeation, the improvement of H2/CO2 separation performance for PBI mixed matrix hollow fibers is hindered at high pressure around 30 bar because of the CO2 adsorption in ZIF-8, which blocks the H2 transport [25]. Song et al. [20] prepared Pebax® 1657/MIL-101 and Pebax® 1657/NH2-MIL-101 MMMs for CO2/N2 separation under sub-ambient condition. Authors found that the Pebax® 1657/NH2-MIL-101 MMM possesses higher CO2/N2 selectivity equal to 95.6 comparing to CO2/N2 selectivity equal to 89.4 for Pebax® 1657/MIL-101 MMM. This is because the amino-modified MIL-101 introduced –NH2 group possessing higher affinity to CO2. Therefore, the solubility and adsorption capacity of CO2 in MMMs were improved [20].
The preparation of flat sheet MMMs containing UiO-66 and UiO-66-NH2 for gas separation has been also studied [14,21,22]. Shen et al. [14] prepared UiO-66/Pebax® 1657 and UiO-66-NH2/Pebax® 1657 flat sheet MMMs for CO2/N2 separation. It was found that the UiO-66-NH2 nanoparticles showed higher affinity to carbon dioxide than UiO-66. The dispersibility of nanoparticles in the polymer matrix was improved due to the enhanced hydrogen bonding between fillers and polymer chains. With MOF loading of 10 wt%, UiO-66-NH2-Pebax® 1657 MMM showed higher CO2/N2 selectivity and slightly lower CO2 permeability than those of UiO-66-Pebax® 1657 membrane [14]. Chuah et al. [21] investigated CO2/N2 separation performance of polyimide-based MMMs containing UiO-66 possessing different functional groups (–HN2, –Br, –(OH)2). It was found that the functionalized UiO-66 in MMMs can effectively increase the CO2 diffusivity while suppressing N2 adsorption [21]. In the above examples, the UiO-66 nanoparticles with various functional groups are synthesized by using pre-synthetic functionalization. It is believed that the further functionalization of UiO-66-NH2 by using post-synthetic functionalization method can further tune the properties of UiO-66-NH2, such as the CO2 affinity and adsorption capacity, pore size, and surface area. Consequently, the CO2 capture ability of MMMs is enhanced [22]. Jiang et al. [22] modified UiO-66-NH2 with imidazole-2-carbaldehyde (ICA) via amine condensation. After modification, the pore volume and BET (Brunauer-Emmett-Teller) area of UiO-66-NH2 were reduced while the CO2 affinity and CO2/CH4 adsorption selectivity were increased. It was found that when 10 wt% modified UiO-66-NH2 was incorporated into Matrimid® membranes, the high CO2/CH4 selectivity of 64.7 was obtained, which is 40% higher than the membranes containing UiO-66-NH2. As aforementioned, the presence of amine groups improved the CO2 adsorption capacity for UiO-66-NH2, resulting in higher CO2 solubility of MMMs, consequently, the higher CO2/N2 selectivity. Moreover, UiO-66-NH2 shows high compatibility with polymer matrix due to the hydrogen bonding between Pebax® chains and UiO-66-NH2. Hence, UiO-66-NH2 was incorporated into Pebax® 2533 matrix to improve the gas separation properties of thin film mixed matrix hollow fiber membranes in this work.
Microporous polypropylene hollow fiber membranes are suitable to be used as a support for the fabrication of composite hollow fiber membranes due to their desirable properties, e.g., high void volumes, well-controlled porosity, chemical inertness, good mechanical strength, and low cost [26]. Therefore, polypropylene hollow fibers were used as supports for the preparation of thin film mixed matrix hollow fiber membranes in this work.
Hollow fiber membranes have a promising future in various gas separation processes due to their advantages, e.g., high packing density and a self-supporting structure [6,7]. However, the flat sheet MMMs have been intensively studied since the incorporation of fillers, e.g., MOF particles can significantly enhance the gas separation performance of polymeric membranes. Therefore, it is highly necessary to investigate the formation of a selective layer containing filler e.g., MOF particles on the hollow fiber support and their gas separation performance. In this work, the main objective is to develop thin film mixed matrix hollow fiber membranes by incorporating UiO-66-NH2 filler into the Pebax® 2533 selective layer. The effect of UiO-66-NH2 filler on the morphology, surface chemistry, and CO2/N2 separation performance of the prepared thin film mixed matrix hollow fiber membranes will be investigated.

2. Experimental

2.1. Materials

Polypropylene (PP) hollow fibers were kindly provided by Faculty of Chemical and Processing Engineering, Warsaw University of Technology (Warsaw, Poland). The PP hollow fibers were prepared via a dry-jet-wet spinning process, using a laboratory made setup. The PP hollow fibers possessed outer diameter of 2.6 mm, internal diameter of 1.8 mm, average pore size of 0.3 µm, and porosity of 50–60% [27]. Pebax® 2533 was provided by Arkema (Colombes, France). Pebax® 2533 consists of poly(ethylene oxide)—PEO block (80 wt%) and polyamide—PA-12 block (20 wt%).
Zirconylchloride octahydrate was supplied by Acbr GmbH (Karlsruhe, Germany). 2-aminoterephthalic acid and N,N-dimethylformamide (DMF) were purchased from Sigma Aldrich (Poznań, Poland). Ethanol was purchased from Alchem Grupa Sp. z o.o. (Toruń, Poland). CO2 (99.999%) and N2 (99.999%) were purchased from Air Products Sp. z o.o. (Siewierz, Poland). The mixing nozzles and epoxy resin were delivered by Farnell (Warsaw, Poland).

2.2. UiO-66-NH2 Synthesis

To synthesize UiO-66-NH2, 4.34 g of 2-aminoterephthalic acid and 7.6 g of zirconylchloride octahydrate were added into 72 mL of DMF. The homogeneous mixture was obtained by stirring (Heating magnetic stirrer, VELP Scientifica, Usmate Velate, Italy) and sonication (BANDELIN SONOREX, BANDELIN electronic GmbH & Co. KG, Berlin, Germany) at room temperature. Then the homogeneous mixture was kept in oven (Memmert GmbH + Co. KG, Schwabach, Germany) at 120 °C for 24 h. Then, the temperature of the mixture decreased to room temperature and centrifuged (High speed centrifuge type 310, Mechanika Precyzyjna, Warsaw, Poland) at 5000 rpm for 15 min. The obtained products were washed three times with DMF and ethanol, respectively. Finally, the obtained products were dried at room temperature and further in the oven at 150 °C for 4 h.

2.3. Fabrication of Pristine Pebax/PP and Pebax® 2533-UiO-66-NH2/PP Thin Film Mixed Matrix Hollow Fiber Membranes

To prepare the pristine Pebax® 2533/PP thin film hollow fiber membranes, Pebax® 2533 pellets were added into ethanol (90 wt%)/water (10 wt%) solvent. After that, the mixture was stirred at 80 °C for 3 h to obtain 3 and 6 wt% polymer solutions. Then, Pebax® 2533 solution was cooled down to 25 °C. The dip-coating technique was used for the preparation of the thin Pebax® 2533 layer on the shell side of the PP hollow fiber supports. First of all, a 10 cm long PP hollow fiber was prepared, and one end of the hollow fiber was sealed with epoxy resin. After the solidification of epoxy resin, the other end of the hollow fiber was attached to a metal holder. Then the single PP hollow fiber was vertically immersed into the 3 wt% Pebax® 2533 solution for 1 min at room temperature. Finally, the Pebax® 2533 coated hollow fiber was slowly taken from the coating solution and dried in air for more than 48 h for solvent evaporation. Afterwards, the second Pebax® 2533 thin layer was formed from 6 wt% Pebax® 2533 solution by using the same dip coating procedure. The preparation of the pristine Pebax® 2533 thin film hollow fiber membrane was schematically illustrated in Figure 1A. The ideal selectivity of Pebax® 2533/PP hollow fiber membranes fabricated by a single layer coating of 3 or 6 wt% Pebax® 2533 solution was very low (Table S1), indicating the formation of defective Pebax® 2533 layer. Therefore, a two-step coating process by using two different concentrations of Pebax® 2533 solution was applied in this research.
To prepare the Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes, a proper amount of UiO-66-NH2 particles were firstly dispersed into the ethanol/water solution (90:10 wt%/wt%) under continuous stirring for 1 h at 80 °C. Then 30 min sonication process was applied to the UiO-66-NH2 suspension for better dispersion of UiO-66-NH2 particles. Afterwards, 10% of the required amount of Pebax® 2533 pellets was added to solvent mixture under continuous stirring for 2 h at 80 °C. Finally, the rest of Pebax® 2533 pellets was dissolved into the solvent mixture under continuous stirring for 12 h at 80 °C to obtain 6 wt% Pebax® 2533 solution containing UiO-66-NH2. The dip coating process for the preparation of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes is the same as for the preparation of pristine Pebax® 2533/PP thin film hollow fiber membranes. The first layer was formed on the PP hollow fiber support from 3 wt% Pebax® 2533 solution, and the second layer was formed from the 6 wt% Pebax® 2533 solution containing UiO-66-NH2. The fabrication of the Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membrane was schematically illustrated in Figure 1B.

2.4. Characterization

The morphology and element mapping of the UiO-66-NH2 particles, PP hollow fibers, Pebax® 2533/PP and mixed matrix Pebax® 2533/PP thin film hollow fiber membranes were analyzed by using scanning electron microscope (SEM) with X-ray spectroscopy (EDX) analysis—Phenom, Generation 5 (Phenom-Word B. V., Eindhoven, The Netherlands). The hollow fiber membranes were fractured in liquid nitrogen (Air Products, Siewierz, Poland) to prepare the samples for the cross-section SEM analysis. The Pebax® 2533 layer thickness was measured on SEM pictures by using ImageJ software (version 1.8.0_172, 2020, University of Wisconsin, Madison, WI, USA).
The surface chemistry of UiO-66-NH2 particles, Pebax® 2533/PP and mixed matrix Pebax/PP thin film hollow fiber membranes were analyzed by using FTIR-ATR spectroscopy. The FTIR-ATR spectra were obtained between 500 and 4000 cm−1 by using spectrometer Nicolet iS10 (Thermal Scientific, Waltham, MA, USA). The transmission mode with resolution of 4 cm−1 and 256 scans was applied. The obtained data was analyzed by Omnic 9 software (Version 9.2, 2012, Thermo Fisher Scientific, Waltham, MA, USA).
The TGA-DTA analyses for UiO-66-NH2 particles were conducted by using TA Instrument type SDT 2960 (TA Instrument, Champaign, IL, USA). The measuring temperature was set in the range of 25–950 °C under nitrogen atmosphere. The heating rate was 10 °C/min. The obtained data were analyzed by using TA Universal Analysis software (version: v5.5.24, 2015, TA Instrument, Champaign, IL, USA).
XRD analyses for UiO-66-NH2 particles were conducted by using Philips X”Pert (Malvern Panalytical, Malvern, UK). The transmission mode was applied. The measured 2θ range was in the range of 5−80°. The X’Celerator Scientific detector (Malvern Panalytical, Malvern, UK) with Cu anode was used.
The nitrogen adsorption/desorption measurements were conducted at −195.7 °C via Gemini VI (Micromeritics Instrument Corp., Norcross, GA, USA). All samples were degassed for 6 h at 110 °C before the measurements. The BET (Brunauer–Emmett–Teller) model was applied for the calculation of surface area.

2.5. Gas Permeance Measurements

To measure the gas permeance of hollow fiber membranes, the hollow fiber membranes should be assembled into the module. The module used for the gas permeance measurements of hollow fiber membranes was designed and assembled by the Membranes and Membrane Techniques Research Group in Nicolaus Copernicus University in Toruń, Toruń, Poland. All parts of the module were purchased from Swagelok (Toruń, Poland) (Figure S1). One hollow fiber with a length of 7–10 cm was assembled into the module. A potting process is needed before the assembling of hollow fiber membrane into the module. The details related to the set-up for gas permeance measurements, and the potting process are described elsewhere [7].
The pure gas (N2 and CO2) permeance tests were conducted at 2 bar and 25 °C. Each sample was measured 3 times under stabilized condition for better accuracy. The gas flow rate was measured by using a bubble flow meter (Sigma Aldrich, Poznań, Poland). The permeances (P/d) of gases were calculated by using Equation (1) [7,8]:
P d = Q Δ pA = Q 2 n π rl Δ p
where P is the permeability (Barrer); Q is the flux of gas permeation rate (cm3 (STP)/s); d is the thickness of membrane selective layer (cm); A is the effective membrane area (cm2); Δp is the pressure difference across the membrane (cmHg); r is the outer radius (cm) of hollow fiber; n is the number of hollow fibers; P/d is the gas permeance expressed in GPU (1 GPU = 10−6 cm3 (STP) cm−2 s−1 cmHg−1).
The ideal selectivity α was calculated by using Equation (2) [7,8]:
α 12 = ( P / d ) 1 ( P / d ) 2 = P 1 P 2

3. Results and Discussion

3.1. Characterization of UiO-66-NH2

The SEM and EDX results of the synthesized UiO-66-NH2 crystals were shown in Figure 2. The UiO-66-NH2 showed octahedrally rectangular shapes [14]. The particle size of UiO-66-NH2 is around 50–80 nm (Figure 2b). The elemental composition of synthesized UiO-66-NH2 was revealed by EDX analysis. UiO-66-NH2 is composed of Zr, C, O, and N elements (Figure 2c). The EDX results are in good agreement with its crystal structure which consists of Zr6-cluster and 2-aminoterephthalic acid linker.
As it is shown in Figure 3, the FTIR spectra provided more information about the chemical structure of the prepared UiO-66-NH2 particles. The intensive peak at 1658 cm−1 is ascribed to the stretching vibration of C=O group from residual DMF solvent in the MOF structure [28]. Two characteristic peaks at 3454 and 333 cm−1 can be ascribed to the asymmetric and symmetric stretching vibration of the primary amine group, respectively [29]. Moreover, the peak at 1620 cm−1 can be ascribed to the N–H bending vibration. What is more, the C–N bonding can be observed at 1257 and 1336 cm−1 due to the stretching vibration of C–N bond. The peak at 764 cm−1 can be assigned to the stretching vibration of Zr–O bond. The peak at 1435 cm−1 can be related to the C–C stretching vibration in the aromatic ring from the 2-aminoterephthalic acid ligand. Moreover, the peaks at 1381 and 1570 cm−1 can be assigned to the symmetric and asymmetric C–O stretching bonds, respectively, resulting from aromatic and carboxylic groups [30].
The TGA and the DTG curves are presented in Figure 4. The DTG curve was plotted as a function of temperature since it can clearly provide information of the transitions of UiO-66-NH2. As it is shown in Figure 4, the TGA and DTG curves of UiO-66-NH2 show a two-step mass loss. The UiO-66-NH2 powder underwent fist-stage mass loss when the temperature increased to 280 °C. This is because the removal of absorbed moisture, residual solvent and the dehyroxylation of the Zr6O4(OH)4 into Zr6O6 [28]. The mass lass at this stage is around 40%. The crystal framework decomposition temperature for UiO-66-NH2 is around 380 °C indicated by the second-stage mass loss. At the second stage of mass loss, the decomposition of amino terephthalic acid ligand occurred and ZrO2 was formed [14]. Finally, when the temperature arrived at 650 °C, UiO-66-NH2 nanoparticles showed the largest mass loss around 68%. Cao et al. [31] also found that the decomposition of amino terephthalic acid ligand in UiO-66-NH2 nanoparticles occurred from 380 °C. When the temperature reaches 650 °C, the UiO-66-NH2 has the largest mass loss of approximately 65% [31]. The N2 adsorption-desorption isotherm measured at 77 K was used to determine the specific area and pore structure of UiO-66-NH2 (Figure 5). The adsorption hysteresis was observed due to the network effects and various forms of pore blocking [32], which could have resulted from the high increasing rate of temperature during the synthesis process. The BET (Brunauer-Emmett-Teller) surface area, adsorption average pore diameter, and BJH (Barrett–Joyner–Halenda) pore volume of the synthesized UiO-66-NH2 were 349.35 m2/g, 2.35 nm, and 0.49 cm3/g, respectively. Our results are in good agreement with the earlier reports [33,34].
The XRD analysis has been performed to prove that UiO-66-NH2 has been successfully synthesized. The formation of MOF was evidenced by the observation of characteristic intensive peaks at 2Theta equal to 7.5° (111) and 8.8° (002) (Figure 6). The experimental results are in a good accordance to the theoretical diffractogram, calculated based on the single crystal data (Figure 6) (ref code: SURKAT, deposit nr: 1405751) [35] with the implementation of Mercury software (Mercury 4. 2. 0., 2019, Cambridge Crystallographic Data Centre, Cambridge, UK).

3.2. Membrane Characterization

The cross-section SEM and surface images of the polypropylene (PP) hollow fiber support, pristine Pebax® 2533 membrane, and thin film mixed matrix hollow fiber membranes were shown in Figure 7. The Pebax® 2533 thin layer was successfully coated on the shell side of PP hollow fibers by using a dip-coating method. As it is shown in Figure 7A, the PP hollow fiber supports possess porous structure (A1 and A2) and porous outer surface (A3 and A4). The porosity of PP hollow fiber is 50–60% and the average pore size is 0.3 µm [27]. After dip-coating with 3 and 6 wt% Pebax® 2533 solutions, a defect-free Pebax® 2533 selective layer was fabricated on the shell side of PP hollow fiber support (Figure 7B). When UiO-66-NH2 was incorporated into the Pebax® 2533 matrix, the thin film mixed matrix membrane was successfully formed on the outer surface of PP hollow fiber support (Figure 7C–G). The loading amount of UiO-66-NH2 nanoparticles did not influence the thickness of Pebax® 2533-UiO-66-NH2 hybrid selective layer since the coating Pebax® 2533 solution was kept constant at 6 wt%. The thickness of the Pebax® 2533-UiO-66-NH2 hybrid selective layer was in the range of 5.40–6.97 µm (Table S2). When comparing the morphology of the prepared hollow fiber membranes, the roughness of the shell side increased with the increase of the UiO-66-NH2 content from 0 to 50 wt% (Figure 7B4–G4). When the content of UiO-66-NH2 was low (5 and 10 wt%), the homogeneous dispersion of UiO-66-NH2 particles into Pebax® 2533 matrix was observed (Figure 7B,C). At the high content of MOF particles (15, 20, and 50 wt%), the aggregation of UiO-66-NH2 in the polymeric matrix was observed (Figure 7E–G and Figure S2). It is reported that the MOF aggregation in polymeric matrix could lead to the formation of non-selective defects during the fabrication process [36]. Similar phenomenon was observed by Sutrisna et al. [33]. In their work, Pebax® 1657-UiO-66/PVDF thin film mixed matrix hollow fiber membranes were prepared for CO2 separation. When the filler content was in the range of 10–50 wt%, no significantly aggregation was observed. However, the significant UiO-66 particle aggregation was observed when 80 wt% of UiO-66 was incorporated into the Pebax® 1657 matrix [33].
To investigate the chemical structure of pure PP hollow fiber support and the prepared thin film mixed matrix hollow fiber membranes, FTIR analysis was conducted. The FTIR spectra of PP hollow fiber support and the prepared Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes in the range of 650–4000 cm−1 were shown in Figure 8. As the FTIR spectra of PP shows, the peak at 841 cm−1 was attributed to C–CH3 stretching vibration. The peaks at 973, 998, and 1168 cm−1 were attributed to –CH3 rocking vibration. The symmetric bending vibration of –CH3 group was observed at 1376 cm−1. The –CH3 asymmetric stretching vibration was observed at 2951 cm−1. Besides the peaks related to methyl group in PP, the peaks at 1456, 2839, and 2919 cm−1 are designated to –CH2– symmetric bending, –CH2– symmetric stretching and –CH2– asymmetric stretching, respectively. Our FTIR results are in good agreement with the literature values [37,38]. After the formation of Pebax® 2533 layer on the shell side of PP hollow fiber support, the characteristic peaks of the –CH3 group from PP disappeared. The characteristic peaks at 1109, 1640, 1734, and 3308 cm−1, are assigned to the stretching vibration of the C–O–C group of the PEO segment part, the N–H–C=O stretching vibration, the –O–C=O group, and the –N–H– stretching vibration of the polyamide block in Pebax® 2533, respectively [33,39]. The FTIR spectra of the prepared Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes are similar to the FTIR spectra of pristine Pebax® 2533/PP hollow fiber membranes, which demonstrates that there were no strong chemical interaction between UiO-66-NH2 fillers and Pebax® 2533 matrix. It was found that the red shift of FTIR characteristic peak related to the –N–H– stretching vibration occurred when the UiO-66-NH2 particles were incorporated into Pebax® 2533 due to the formation of hydrogen bonding [14,40]. However, the peaks related to the –N–H– stretching vibration for the mixed matrix membrane containing 0, 5, 10, 15, 20, and 50 wt% of UiO-66-NH2 are 3308, 3297, 3297, 3296, 3307, and 3307 cm−1, respectively (Figure 8A). The –N–H– peak shift for PA (polyamide) segment is negligible due to the difficulty in the thin composite layer characterization [33]. As it is shown in the FTIR spectra in the range of 700–800 cm−1 (Figure 8C), a peak related to the stretching vibration of Zr–O bond around 764 cm−1 was observed, which indicates the serious aggregation of UiO-66-NH2 particles in the mixed matrix hollow fiber membranes. This finding is in good agreement with the SEM results (Figure 7G).

3.3. The Effect of UiO-66-NH2 Loading on Gas Separation Performance

The gas separation behaviors of the prepared thin film mixed matrix hollow fiber membranes were studied by the gas permeation measurements. The CO2 and N2 permeance through the prepared membranes were measured at 2 bar and 25 °C. As it is shown in Figure 9, the UiO-66-NH2 content in the Pebax® 2533 matrix influenced the gas permeance and the ideal selectivity of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes. As can be seen from Figure 9A, when the UiO-66-NH2 content increased from 0 to 50 wt%, the CO2 permeance increased significantly from 19 to 30 GPU. The N2 permeance barely increased when the UiO-66-NH2 content increased from 0 to 10 wt%. However, the N2 permeance increased to 0.91, 1.14, and 1.42 GPU when the UiO-66-NH2 content increased to 15, 20, and 50 wt%, respectively. As it is shown in Figure 9B, the CO2/N2 ideal selectivity firstly increased from 30 to 37 when the UiO-66-NH2 content increased from 0 to 10 wt%. Then the CO2/N2 ideal selectivity decreased to 21 when the UiO-66-NH2 content increased to 50 wt%.
As discussed above, when the UiO-66-NH2 content increased to 10 wt%, both the CO2 permeance and CO2/N2 ideal selectivity increased while the N2 permeance was practically unchanged, which indicates the formation of defect-free thin mixed matrix membrane on the PP hollow fiber support. The enhanced CO2 permeance and CO2/N2 ideal selectivity were ascribed to the interrupted chain packing in the polymer matrix [41] and the CO2-philic nature of UiO-66-NH2 [42]. In comparison to the pure Pebax® 2533 thin film hollow fiber membrane, the CO2 permeance and CO2/N2 ideal selectivity of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membrane containing 10 wt% UiO-66-NH2 increased by 35 and 23%, respectively. The kinetic diameters for CO2 and N2 molecules are 0.33 and 0.36 nm, respectively. The CO2 mobility is higher than the N2 mobility in Pebax® membranes due to smaller size and higher condensability of CO2 molecules, and the CO2-philic ether group in Pebax® polymer chains [14]. The CO2 permeance increased with the addition of UiO-66-NH2 nanoparticles. The N2 permeance increased slightly when the UiO-66-NH2 content increased from 0 to 10 wt%. However, when the UiO-66-NH2 content was higher than 10 wt%, the N2 permeance started to increase significantly, resulting in the decrease in CO2/N2 ideal selectivity. For instance, when 20 and 50 wt% of UiO-66-NH2 was incorporated into the Pebax® 2533 matrix, the CO2 permeance increased 9% while the N2 permeance increased 25%. Consequently, the CO2/N2 ideal selectivity was less than that of pure Pebax® 2533 membranes. This can be explained by the severe agglomeration of UiO-66-NH2 when large amounts of UiO-66-NH2 particles were incorporated into polymeric matrix. Consequently, the non-selective interface defects were formed, resulting in the deterioration of gas separation of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes. The agglomeration of nanoparticles in the mixed matrix membranes have been documented in the literature [14,41,43]. Shen et al. [14] prepared Pebax® 1657 based mixed matrix membranes containing UiO-66 and UiO-66-NH2 nanoparticles for CO2 separation. It was found that CO2/N2 selectivity started to decrease due to the filler agglomeration when the UiO-66 and UiO-66-NH2 loading is higher than 7.5 and 10 wt%, respectively. Jiao et al. [43] synthesized polyethyleneimine (PEI) modified ZIF-8 and incorporated the PEI-ZIF-8 particle into Pebax® 1657 matrix to prepare mixed matrix membranes for CO2/N2 separation. It was found that the composite membrane with 5 wt% PEI-ZIF-8 shows the best gas separation performance with CO2 permeance equal to 13 GPU and CO2/N2 selectivity equal to 49. The filler agglomeration occurred resulting in rigidified interface.

3.4. Comparison of the Pebax®-Based Mixed Matrix Membranes Incorporating Various Nanoparticles in CO2/N2 Gas Separation

The performance of the prepared Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes were compared with Pebax®-based mixed matrix membranes containing various types of fillers (Table 1). The gas separation performance of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membrane containing 10 wt% UiO-66-NH2 is comparable with previous reported Pebax®-based mixed matrix membranes containing various types of fillers in literature [14,33,40,44,45,46,47,48,49,50,51,52]. The prepared membrane shows a high CO2/N2 ideal selectivity equal to 37 with a CO2 permeance 25.81 GPU at feed pressure 2 bar. The addition of UiO-66-NH2 enhances the CO2/N2 separation performance mainly due to the good interfacial compatibility and the CO2-philic nature of UiO-66-NH2. Sutrisna et al. [33] fabricated UiO-66-NH2/Pebax® 1657 based hollow fiber composite membranes with high CO2 permeance equal to 338 GPU and high CO2/N2 selectivity equal to 57. Their work showed better CO2/N2 separation performance, which can be attributed to the lower Pebax® 1657 coating solution, and the application of poly [1-(trimethylsilyl) prop-1-yne] (PTMSP) as a gutter layer. The lower coating solution concentration could result in smaller selective layer thickness. The smooth PTMSP gutter layer can prevent the intrusion of Pebax® into pores of support layer, resulting in a thin selective layer. As a result, the prepared UiO-66-NH2/Pebax® 1657 based hollow fiber composite membranes showed very high gas separation performance. As it is shown in Table 1, the thin film mixed matrix membranes possess comparable CO2/N2 selectivity but much higher CO2 permeance than that of dense flat sheet mixed matrix membranes. Therefore, the gas separation performances of thin film mixed matrix membranes are better than the dense flat sheet membranes.

4. Conclusions

Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membranes were successfully fabricated by using dip coating method. The pre-treatment of PP hollow fibers by dip-coating with 3 wt% Pebax® 2533 solution could smoothen the outer surface of hollow fiber supports, which facilitated the formation of defect-free selective layer. The incorporation of UiO-66-NH2 nanoparticles into the Pebax® 2533 coating solution affected the morphology, surface chemistry, and gas separation performance of Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membranes confirmed by SEM analysis, FTIR analysis, and gas permeance measurements, respectively. The aggregation of UiO-66-NH2 nanoparticles was observed at higher amounts of UiO-66-NH2 nanoparticles in the Pebax® 2533 matrix. The filler aggregation should be tackled by post-synthetic modification of UiO-66-NH2 nanoparticles. The CO2 permeance increased with the increase of the loading amount of UiO-66 nanoparticles, while the CO2/N2 ideal gas selectively firstly increased then decreased due to the aggregation of UiO-66 nanoparticles. The Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membranes containing 10 wt% UiO-66 nanoparticles exhibited the best gas separation performance with CO2 permeance of 26 GPU and CO2/N2 selectivity of 37.

Supplementary Materials

The following are available online at https://www.mdpi.com/article/10.3390/ma14123366/s1, Figure S1: Hollow fiber module for testing gas permeance of hollow fiber membranes (This module is designed by the Membranes and Membrane Techniques Research Group in Nicolaus Copernicus University in Toruń. All the components of this module including housing part, end caps, and ports are purchased from Swagelok), Figure S2: The Zr element mapping and element analysis of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes by EDX. (a) 15 wt% UiO-66-NH2, (b) 20 wt% UiO-66-NH2, (c) 50 wt% UiO-66-NH2, Table S1: The gas permeance and ideal selectivity of thin film hollow fiber membranes fabricated from single concentration of coating solution, Table S2: The thickness of the Pebax/UiO-66-NH2 hybrid layer measured from the top part and bottom part of the prepared mixed matrix thin film hollow fiber membrane. The bottom part is close to the coating solution while the top part is close to the metal holder during the dip-coating process.

Author Contributions

Conceptualization, G.L. and W.K.; Data curation, G.L. and K.K.; Formal analysis, G.L., W.K., K.K. and J.K.; Funding acquisition, G.L. and W.K.; Investigation, G.L.; Methodology, G.L., W.K. and J.K.; Resources, W.K.; Software, K.K. and J.K.; Supervision, W.K. and J.K.; Validation, G.L.; Visualization, G.L. and K.K.; Writing—original draft, G.L.; Writing—review & editing, G.L., W.K. and K.K. All authors have read and agreed to the published version of the manuscript.

Funding

This work was supported by the Young Researcher grant for PhD Students of Nicolaus Copernicus University in Toruń, Poland (Faculty of Chemistry, 492/2020).

Institutional Review Board Statement

Not applicable.

Informed Consent Statement

Not applicable.

Data Availability Statement

The data presented in this study are available on request from the corresponding author.

Conflicts of Interest

The authors declare no conflict of interest.

References

  1. Al Mesfer, M.K.; Danish, M. Breakthrough adsorption study of activated carbons for CO2 separation from flue gas. J. Environ. Chem. Eng. 2018, 6, 4514–4524. [Google Scholar] [CrossRef]
  2. Wang, K.; Xu, H.; Yang, C.; Qiu, T. Machine learning-based ionic liquids design and process simulation for CO2 separation from flue gas. Green Energy Environ. 2020. [Google Scholar] [CrossRef]
  3. Polat, H.M.; Kavak, S.; Kulak, H.; Uzun, A.; Keskin, S. CO2 separation from flue gas mixture using [BMIM][BF4]/MOF com-posites: Linking high-throughput computational screening with experiments. Chem. Eng. J. 2020, 394, 124916. [Google Scholar] [CrossRef]
  4. Gilassi, S.; Taghavi, S.M.; Rodrigue, D.; Kaliaguine, S. Techno-Economic Analysis of a Hybrid System for Flue-Gas Separa-tion: Combining Membrane and Enzymatic-Absorption Processes. Chem. Eng. Process. Process. Intensif. 2021, 159, 108222. [Google Scholar] [CrossRef]
  5. Kamble, A.R.; Patel, C.M.; Murthy, Z. A review on the recent advances in mixed matrix membranes for gas separation processes. Renew. Sustain. Energy Rev. 2021, 145, 111062. [Google Scholar] [CrossRef]
  6. Li, G.; Kujawski, W.; Válek, R.; Koter, S. A review—The development of hollow fibre membranes for gas separation processes. Int. J. Greenh. Gas. Control. 2021, 104, 103195. [Google Scholar] [CrossRef]
  7. Li, G.; Kujawski, W.; Knozowska, K.; Kujawa, J. The Effects of PEI Hollow Fiber Substrate Characteristics on PDMS/PEI Hollow Fiber Membranes for CO2/N2 Separation. Membranes 2021, 11, 56. [Google Scholar] [CrossRef]
  8. Li, G.; Knozowska, K.; Kujawa, J.; Tonkonogovas, A.; Stankevičius, A.; Kujawski, W. Fabrication of Polydimethysiloxane (PDMS) Dense Layer on Polyetherimide (PEI) Hollow Fiber Support for the Efficient CO2/N2 Separation Membranes. Polymers 2021, 13, 756. [Google Scholar] [CrossRef] [PubMed]
  9. Liu, B.; Tang, C.; Li, X.; Wang, B.; Zhou, R. High-performance SAPO-34 membranes for CO2 separations from simulated flue gas. Microporous Mesoporous Mater. 2020, 292, 109712. [Google Scholar] [CrossRef]
  10. Ilicak, I.; Boroglu, M.S.; Durmus, A.; Boz, I. Influence of ZIF-95 on structure and gas separation properties of polyi-mide-based mixed matrix membranes. J. Nat. Gas. Sci. Eng. 2021, 91, 103941. [Google Scholar] [CrossRef]
  11. Wang, Q.; Dai, Y.; Ruan, X.; Zheng, W.; Yan, X.; Li, X.; He, G. ZIF-8 hollow nanotubes based mixed matrix membranes with high-speed gas transmission channel to promote CO2/N2 separation. J. Membr. Sci. 2021, 630, 119323. [Google Scholar] [CrossRef]
  12. Saqib, S.; Rafiq, S.; Muhammad, N.; Khan, A.L.; Mukhtar, A.; Ullah, S.; Nawaz, M.H.; Jamil, F.; Zhang, C.; Ashokkumar, V. Sustainable mixed matrix membranes containing porphyrin and polysulfone polymer for acid gas separations. J. Hazard. Mater. 2021, 411, 125155. [Google Scholar] [CrossRef]
  13. Liu, L.; Chakma, A.; Feng, X. CO2/N2 Separation by Poly(Ether Block Amide) Thin Film Hollow Fiber Composite Membranes. Ind. Eng. Chem. Res. 2005, 44, 6874–6882. [Google Scholar] [CrossRef]
  14. Shen, J.; Liu, G.; Huang, K.; Li, Q.; Guan, K.; Li, Y.; Jin, W. UiO-66-polyether block amide mixed matrix membranes for CO2 separation. J. Membr. Sci. 2016, 513, 155–165. [Google Scholar] [CrossRef]
  15. Casadei, R.; Baschetti, M.G.; Yoo, M.J.; Park, H.B.; Giorgini, L. Pebax® 2533/Graphene Oxide Nanocomposite Membranes for Carbon Capture. Membranes 2020, 10, 188. [Google Scholar] [CrossRef] [PubMed]
  16. Liu, C.; Wang, J.; Wan, J.; Yu, C. MOF-on-MOF hybrids: Synthesis and applications. Co-Ord. Chem. Rev. 2021, 432, 213743. [Google Scholar] [CrossRef]
  17. Chen, S.; Li, X.; Duan, J.; Fu, Y.; Wang, Z.; Zhu, M.; Li, N. Investigation of highly efficient adsorbent based on Ni-MOF-74 in the separation of CO2 from natural gas. Chem. Eng. J. 2021, 419, 129653. [Google Scholar] [CrossRef]
  18. Kujawa, J.; Al-Gharabli, S.; Muzioł, T.M.; Knozowska, K.; Li, G.; Dumée, L.F.; Kujawski, W. Crystalline porous frameworks as nano-enhancers for membrane liquid separation—Recent developments. Co-Ord. Chem. Rev. 2021, 440, 213969. [Google Scholar] [CrossRef]
  19. Gao, J.; Mao, H.; Jin, H.; Chen, C.; Feldhoff, A.; Li, Y. Functionalized ZIF-7/Pebax® 2533 mixed matrix membranes for CO2/N2 separation. Microporous Mesoporous Mater. 2020, 297, 110030. [Google Scholar] [CrossRef]
  20. Song, C.; Li, R.; Fan, Z.; Liu, Q.; Zhang, B.; Kitamura, Y. CO2/N2 separation performance of Pebax/MIL-101 and Pebax /NH2-MIL-101 mixed matrix membranes and intensification via sub-ambient operation. Sep. Purif. Technol. 2020, 238, 116500. [Google Scholar] [CrossRef]
  21. Chuah, C.Y.; Lee, J.; Song, J.; Bae, T.-H. CO2/N2 Separation Properties of Polyimide-Based Mixed-Matrix Membranes Comprising UiO-66 with Various Functionalities. Membranes 2020, 10, 154. [Google Scholar] [CrossRef] [PubMed]
  22. Jiang, Y.; Liu, C.; Caro, J.; Huang, A. A new UiO-66-NH2 based mixed-matrix membranes with high CO2/CH4 separation performance. Microporous Mesoporous Mater. 2019, 274, 203–211. [Google Scholar] [CrossRef]
  23. Jameh, A.A.; Mohammadi, T.; Bakhtiari, O. Preparation of PEBAX-1074/modified ZIF-8 nanoparticles mixed matrix membranes for CO2 removal from natural gas. Sep. Purif. Technol. 2020, 231, 115900. [Google Scholar] [CrossRef]
  24. Dai, Y.; Johnson, J.; Karvan, O.; Sholl, D.S.; Koros, W. Ultem®/ZIF-8 mixed matrix hollow fiber membranes for CO2/N2 separations. J. Membr. Sci. 2012, 401–402, 76–82. [Google Scholar] [CrossRef]
  25. Etxeberria-Benavides, M.; Johnson, T.; Cao, S.; Zornoza, B.; Coronas, J.; Sanchez-Lainez, J.; Sabetghadam, A.; Liu, X.; Andres-Garcia, E.; Kapteijn, F.; et al. PBI mixed matrix hollow fiber membrane: Influence of ZIF-8 filler over H2/CO2 separation performance at high temperature and pressure. Sep. Purif. Technol. 2020, 237, 116347. [Google Scholar] [CrossRef]
  26. Xu, Z.-K.; Dai, Q.-W.; Liu, Z.-M.; Kou, R.-Q.; Xu, Y.-Y. Microporous polypropylene hollow fiber membranes: Part II. Per-vaporation separation of water/ethanol mixtures by the poly (acrylic acid) grafted membranes. J. Membr. Sci. 2003, 214, 71–81. [Google Scholar] [CrossRef]
  27. Szwast, M.; Zalewski, M.; Prokopowicz, L.; Khoshgrudi, R.N. Novel Mixed Matrix Membrane for gas mixture separation. In Monographs of the Environmental Engineering Committee Polish Academy of Sciences: Membranes and Membrane Processes in Environmental Protection; Konieczny, K., Korus, I., Eds.; Polska Akademia Nauk, Komitet Inżynierii Środowiska: Warsaw, Poland, 2014; pp. 89–99. [Google Scholar]
  28. Zhu, J.; Wu, L.; Bu, Z.; Jie, S.; Li, B.-G. Polyethyleneimine-Modified UiO-66-NH2(Zr) Metal–Organic Frameworks: Preparation and Enhanced CO2 Selective Adsorption. ACS Omega 2009, 4, 3188–3197. [Google Scholar] [CrossRef] [Green Version]
  29. Hou, J.; Luan, Y.; Tang, J.; Wensley, A.M.; Yang, M.; Lu, Y. Synthesis of UiO-66-NH2 derived heterogeneous copper (II) catalyst and study of its application in the selective aerobic oxidation of alcohols. J. Mol. Catal. A Chem. 2015, 407, 53–59. [Google Scholar] [CrossRef]
  30. Zhang, X.; Zhang, Y.; Wang, T.; Fan, Z.; Zhang, G. A thin film nanocomposite membrane with pre-immobilized UiO-66-NH2 toward enhanced nanofiltration performance. RSC Adv. 2019, 9, 24802–24810. [Google Scholar] [CrossRef] [Green Version]
  31. Cao, Y.; Zhang, H.; Song, F.; Huang, T.; Ji, J.; Zhong, Q.; Chu, W.; Xu, Q. UiO-66-NH2/GO Composite: Synthesis, Characterization and CO2 Adsorption Performance. Materials 2018, 11, 589. [Google Scholar] [CrossRef]
  32. Thommes, M.; Kaneko, K.; Neimark, A.V.; Olivier, J.P.; Rodriguez-Reinoso, F.; Rouquerol, J.; Sing, K.S.W. Physisorption of gases, with special reference to the evaluation of surface area and pore size distribution (IUPAC Technical Report). Pure Appl. Chem. 2015, 87, 1051–1069. [Google Scholar] [CrossRef] [Green Version]
  33. Sutrisna, P.D.; Hou, J.; Zulkifli, M.Y.; Li, H.; Zhang, Y.; Liang, W.; D’Alessandro, D.M.; Chen, V. Surface functionalized UiO-66/Pebax-based ultrathin composite hollow fiber gas separation membranes. J. Mater. Chem. A 2017, 6, 918–931. [Google Scholar] [CrossRef]
  34. Tambat, S.N.; Sane, P.K.; Suresh, S.; Varadan, N.; Pandit, A.B.; Sontakke, S.M. Hydrothermal synthesis of NH2-UiO-66 and its application for adsorptive removal of dye. Adv. Powder Technol. 2018, 29, 2626–2632. [Google Scholar] [CrossRef]
  35. Trickett, C.A.; Gagnon, K.J.; Lee, S.; Gándara, F.; Bürgi, H.-B.; Yaghi, O.M. Definitive Molecular Level Characterization of Defects in UiO-66 Crystals. Angew. Chem. Int. Ed. 2015, 54, 11162–11167. [Google Scholar] [CrossRef] [PubMed]
  36. Bi, X.; Zhang, Y.; Zhang, F.; Zhang, S.; Wang, Z.; Jin, J. MOF Nanosheet-Based Mixed Matrix Membranes with Metal–Organic Coordination Interfacial Interaction for Gas Separation. ACS Appl. Mater. Interfaces 2020, 12, 49101–49110. [Google Scholar] [CrossRef]
  37. Gopanna, A.; Mandapati, R.N.; Thomas, S.P.; Rajan, K.; Chavali, M. Fourier transform infrared spectroscopy (FTIR), Raman spectroscopy and wide-angle X-ray scattering (WAXS) of polypropylene (PP)/cyclic olefin copolymer (COC) blends for qualitative and quantitative analysis. Polym. Bull. 2019, 76, 4259–4274. [Google Scholar] [CrossRef]
  38. Gonzalez-Canche, N.G.; Flores-Johnson, E.A.; Cortes, P.; Carrillo, J.G. Evaluation of surface treatments on 5052-H32 aluminum alloy for enhancing the interfacial adhesion of thermoplastic-based fiber metal laminates. Int. J. Adhes. Adhes. 2018, 82, 90–99. [Google Scholar] [CrossRef]
  39. Bernardo, P.; Clarizia, G. Enhancing Gas Permeation Properties of Pebax® 1657 Membranes via Polysorbate Nonionic Surfactants Doping. Polymers 2020, 12, 253. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  40. Sutrisna, P.D.; Hou, J.; Li, H.; Zhang, Y.; Chen, V. Improved operational stability of Pebax-based gas separation membranes with ZIF-8: A comparative study of flat sheet and composite hollow fibre membranes. J. Membr. Sci. 2017, 524, 266–279. [Google Scholar] [CrossRef]
  41. Nafisi, V.; Hägg, M.-B. Development of dual layer of ZIF-8/PEBAX-2533 mixed matrix membrane for CO2 capture. J. Membr. Sci. 2014, 459, 244–255. [Google Scholar] [CrossRef]
  42. Biswas, S.P.; Van Der Voort, P. A General Strategy for the Synthesis of Functionalised UiO-66 Frameworks: Characterisation, Stability and CO2 Adsorption Properties. Eur. J. Inorg. Chem. 2013, 2013, 2154–2160. [Google Scholar] [CrossRef]
  43. Jiao, C.; Li, Z.; Li, X.; Wu, M.; Jiang, H. Improved CO2/N2 separation performance of Pebax composite membrane containing polyethyleneimine functionalized ZIF-8. Sep. Purif. Technol. 2021, 259, 118190. [Google Scholar] [CrossRef]
  44. Li, Y.; Wang, S.; Wu, H.; Wang, J.; Jiang, Z. Bioadhesion-inspired polymer–inorganic nanohybrid membranes with enhanced CO2 capture properties. J. Mater. Chem. 2012, 22, 19617–19620. [Google Scholar] [CrossRef]
  45. Li, T.; Pan, Y.; Peinemann, K.-V.; Lai, Z. Carbon dioxide selective mixed matrix composite membrane containing ZIF-7 nano-fillers. J. Membr. Sci. 2013, 425-426, 235–242. [Google Scholar] [CrossRef]
  46. Zhang, Y.; Shen, Q.; Hou, J.; Sutrisna, P.D.; Chen, V. Shear-aligned graphene oxide laminate/Pebax ultrathin composite hollow fiber membranes using a facile dip-coating approach. J. Mater. Chem. A 2017, 5, 7732–7737. [Google Scholar] [CrossRef]
  47. Roslan, R.A.; Lau, W.J.; Lai, G.S.; Zulhairun, A.K.; Yeong, Y.F.; Ismail, A.F.; Matsuura, T. Impacts of Multilayer Hybrid Coating on PSF Hollow Fiber Membrane for Enhanced Gas Separation. Membranes 2020, 10, 335. [Google Scholar] [CrossRef] [PubMed]
  48. Zheng, W.; Ding, R.; Yang, K.; Dai, Y.; Yan, X.; He, G. ZIF-8 nanoparticles with tunable size for enhanced CO2 capture of Pebax based MMMs. Sep. Purif. Technol. 2019, 214, 111–119. [Google Scholar] [CrossRef]
  49. Meshkat, S.; Kaliaguine, S.; Rodrigue, D. Mixed matrix membranes based on amine and non-amine MIL-53(Al) in Pebax® MH-1657 for CO2 separation. Sep. Purif. Technol. 2018, 200, 177–190. [Google Scholar] [CrossRef]
  50. Zheng, Y.; Wu, Y.; Zhang, B.; Wang, Z. Preparation and characterization of CO2-selective Pebax/NaY mixed matrix membranes. J. Appl. Polym. Sci. 2020, 137, 48398. [Google Scholar] [CrossRef]
  51. Dong, L.; Chen, M.; Li, J.; Shi, D.; Dong, W.; Li, X.; Bai, Y. Metal-organic framework-graphene oxide composites: A facile method to highly improve the CO2 separation performance of mixed matrix membranes. J. Membr. Sci. 2016, 520, 801–811. [Google Scholar] [CrossRef]
  52. Zhang, X.; Zhang, T.; Wang, Y.; Li, J.; Liu, C.; Li, N.; Liao, J. Mixed-matrix membranes based on Zn/Ni-ZIF-8-PEBA for high performance CO2 separation. J. Membr. Sci. 2018, 560, 38–46. [Google Scholar] [CrossRef]
Materials 14 03366 g001 550
Figure 1. Schematic illustration of the preparation pristine Pebax® 2533 thin film hollow fiber membrane (A) and Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membrane (B).
Figure 1. Schematic illustration of the preparation pristine Pebax® 2533 thin film hollow fiber membrane (A) and Pebax® 2533-UiO-66-NH2/PP mixed matrix thin film hollow fiber membrane (B).
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Figure 2. SEM (scanning electron microscope) images of synthesized UiO-66-NH2 particles (a,b). (c) is the corresponding EDX (energy-dispersive X-ray spectroscopy) data and mapping results of the selected area in (a) of UiO-66-NH2 particles.
Figure 2. SEM (scanning electron microscope) images of synthesized UiO-66-NH2 particles (a,b). (c) is the corresponding EDX (energy-dispersive X-ray spectroscopy) data and mapping results of the selected area in (a) of UiO-66-NH2 particles.
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Figure 3. FTIR (fourier transform infrared) spectra of UiO-66-NH2.
Figure 3. FTIR (fourier transform infrared) spectra of UiO-66-NH2.
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Figure 4. TGA (thermal gravimetric analysis) curves of UiO-66-NH2.
Figure 4. TGA (thermal gravimetric analysis) curves of UiO-66-NH2.
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Figure 5. N2 adsorption and desorption curves of UiO-66-NH2.
Figure 5. N2 adsorption and desorption curves of UiO-66-NH2.
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Figure 6. XRD (X-Ray diffraction) pattern of UiO-66-NH2 (the blue curve) and the theoretical XRD pattern of UiO-66 MOF (metal-organic frameworks) (the red curve).
Figure 6. XRD (X-Ray diffraction) pattern of UiO-66-NH2 (the blue curve) and the theoretical XRD pattern of UiO-66 MOF (metal-organic frameworks) (the red curve).
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Figure 7. SEM pictures of cross-section (1 and 2) and outer surface (3 and 4) of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes—(A) PP hollow fiber support, (B) 0 wt% UiO-66-NH2, (C) 5 wt% UiO-66-NH2, (D) 10 wt% UiO-66-NH2, (E) 15 wt% UiO-66-NH2, (F) 20 wt% UiO-66-NH2, and (G) 50 wt% UiO-66-NH2.
Figure 7. SEM pictures of cross-section (1 and 2) and outer surface (3 and 4) of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes—(A) PP hollow fiber support, (B) 0 wt% UiO-66-NH2, (C) 5 wt% UiO-66-NH2, (D) 10 wt% UiO-66-NH2, (E) 15 wt% UiO-66-NH2, (F) 20 wt% UiO-66-NH2, and (G) 50 wt% UiO-66-NH2.
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Figure 8. FTIR (Fourier transform infrared) spectra of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes (A) (the enlarged FTIR spectra in the wavelength range 3400–3200 cm−1 and 800–700 cm−1 are shown in (B) and (C), respectively).
Figure 8. FTIR (Fourier transform infrared) spectra of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes (A) (the enlarged FTIR spectra in the wavelength range 3400–3200 cm−1 and 800–700 cm−1 are shown in (B) and (C), respectively).
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Figure 9. The effect of UiO-66-NH2 content on the CO2 and N2 permeances (A) and CO2/N2 ideal selectivity (B) of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes.
Figure 9. The effect of UiO-66-NH2 content on the CO2 and N2 permeances (A) and CO2/N2 ideal selectivity (B) of Pebax® 2533-UiO-66-NH2/PP thin film mixed matrix hollow fiber membranes.
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Table
Table 1. The comparison of gas separation performances of Pebax®-based mixed matrix membranes with different fillers.
Table 1. The comparison of gas separation performances of Pebax®-based mixed matrix membranes with different fillers.
Support
Polymer		Hybrid Coating
Material		Filler Content (wt%)ConfigurationFeed GasCO2
(GPU)		N2
(GPU)		CO2/N2
Selectivity		Ref.
PVDF/PTMSPUiO-66-NH2/Pebax® 165750Hollow fiberPure gas3385.9357[33]
PSFFe(DA)/Pebax® 16573Hollow fiberPure gas90.001.6156[44]
PVDFZIF-8/Pebax® 165730Hollow fiberPure gas350.0010.9432[40]
PVDFGO/Pebax® 16570.1Hollow fiberPure gas415.009.6543[46]
PSFGO/Pebax® 16570.4Hollow fiberPure gas28.080.6643[47]
PANZIF-7/Pebax® 165734Flat sheetPure gas39.000.37105[45]
PVDFUiO-66-NH2/Pebax® 165720Flat sheetPure gas125 Barrer-25[14]
-ZIF-8/Pebax® 165720Dense flat sheetPure gas2.800.0741[48]
-NH2-MIL-53/Pebax® 165710Dense flat sheetPure gas1.600.0355[49]
-NaY/Pebax® 165710Dense flat sheetPure gas3.600.1035[50]
-ZIF-7/Pebax® 253314Dense flat sheetPure gas198 Barrer8.74 Barrer22.6[19]
-ZIF-7-NH2/Pebax® 253314Dense flat sheetPure gas206 Barrer7.53 Barrer27.3[19]
-ZIF-8@GO/Pebax® 25336Dense flat sheetPure gas249 Barrer5.23 Barrer47.6[51]
-Zn/Ni-ZIF-8/Pebax® 253310Dense flat sheetPure gas321 Barrer7.5
Barrer		42.8[52]
PPUiO-66-NH2/Pebax® 253310Hollow fiberPure gas25.810.6937This work
PVDF—polyvinylidene difluoride, PTMSP—poly [1-(trimethylsilyl) prop-1-yne], PSF—polysulfone, PAN—polyacrylonitrile, PP—polypropylene.
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Li, G.; Kujawski, W.; Knozowska, K.; Kujawa, J. Thin Film Mixed Matrix Hollow Fiber Membrane Fabricated by Incorporation of Amine Functionalized Metal-Organic Framework for CO2/N2 Separation. Materials 2021, 14, 3366. https://doi.org/10.3390/ma14123366

AMA Style

Li G, Kujawski W, Knozowska K, Kujawa J. Thin Film Mixed Matrix Hollow Fiber Membrane Fabricated by Incorporation of Amine Functionalized Metal-Organic Framework for CO2/N2 Separation. Materials. 2021; 14(12):3366. https://doi.org/10.3390/ma14123366

Chicago/Turabian Style

Li, Guoqiang, Wojciech Kujawski, Katarzyna Knozowska, and Joanna Kujawa. 2021. "Thin Film Mixed Matrix Hollow Fiber Membrane Fabricated by Incorporation of Amine Functionalized Metal-Organic Framework for CO2/N2 Separation" Materials 14, no. 12: 3366. https://doi.org/10.3390/ma14123366

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