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Article

Highly Selective Oxygen/Nitrogen Separation Membrane Engineered Using a Porphyrin-Based Oxygen Carrier

by
Jiuli Han
1,2,
Lu Bai
1,
Bingbing Yang
1,2,
Yinge Bai
1,
Shuangjiang Luo
1,
Shaojuan Zeng
1,
Hongshuai Gao
1,
Yi Nie
1,3,
Xiaoyan Ji
4,
Suojiang Zhang
1,2,* and
Xiangping Zhang
1,2,*
1
Beijing Key Laboratory of Ionic Liquids Clean Process, State Key Laboratory of Multiphase Complex Systems, CAS Key Laboratory of Green Process and Engineering, Institute of Process Engineering, Chinese Academy of Sciences, Beijing 100190, China
2
School of Chemical Engineering, University of Chinese Academy of Sciences, Beijing 100049, China
3
Zhengzhou Institute of Emerging Industrial Technology, Zhengzhou 450000, China
4
Energy Engineering, Division of Energy Science, Luleå University of Technology, 97187 Luleå, Sweden
*
Authors to whom correspondence should be addressed.
Membranes 2019, 9(9), 115; https://doi.org/10.3390/membranes9090115
Submission received: 16 August 2019 / Revised: 30 August 2019 / Accepted: 30 August 2019 / Published: 3 September 2019
(This article belongs to the Section Membrane Processing and Engineering)
Browse Figures
Versions Notes

Abstract

:
Air separation is very important from the viewpoint of the economic and environmental advantages. In this work, defect-free facilitated transport membranes based on poly(amide-12-b-ethylene oxide) (Pebax-2533) and tetra(p-methoxylphenyl)porphyrin cobalt chloride (T(p-OCH3)PPCoCl) were fabricated in systematically varied compositions for O2/N2 separation. T(p-OCH3)PPCoCl was introduced as carriers that selectively and reversibly interacted with O2 and facilitated O2 transport in the membrane. The T(p-OCH3)PPCoCl had good compatibility with the Pebax-2533 via the hydrogen bond interaction and formed a uniform and thin selective layer on the substrate. The O2 separation performance of the thin film composite (TFC) membranes was improved by adding a small amount of the T(p-OCH3)PPCoCl and decreasing the feed pressure. At the pressure of 0.035 MPa, the O2 permeability and O2/N2 selectivity of the 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 was more than 3.5 times that of the Pebax-2533 TFC membrane, which reached the 2008 Robeson upper bound. It provides a candidate membrane material for O2/N2 efficient separation in moderate conditions.

Graphical Abstract

1. Introduction

Air separation is an essential process, in which the obtained oxygen-enriched air can be used to assist combustion by increasing the burning velocities [1], regenerate catalysts in the fluid catalytic cracking [2], and improve indoor air quality [3]; meanwhile, the obtained nitrogen-enriched air can be applied in keeping food fresh, preventing fires, oil recovery, and draining water [4,5]. Currently, cryogenic distillation is the commercial and mature technology for air separation, which can produce a large amount of high purity (>99%) oxygen and nitrogen. However, this process is complex, as well as cost and energy intensive [6]. Pressure swing adsorption (PSA) is another commonly used air separation method that can produce high purity (≈95%) oxygen with medium production, but the larger space, higher investment, and energy consumption of the process are still challenging [7]. Compared with these air separation technologies, the membrane gas separation method is a green and sustainable process because of its continuous production, easy operation, small space, environmental friendliness, and energy conservation [7,8,9,10,11]. Polymeric membranes are usually applied for air separation, but their gas separation performance is always limited by the Robeson upper bound between O2 permeability and O2/N2 selectivity [12]. Therefore, developing membranes with both excellent O2 permeability and O2/N2 selectivity for efficient air separation is highly desired.
Facilitated oxygen transport through membranes is an effective approach to enhance the separation performance or even overcome the Robeson upper bound. These membranes usually contain metal complexes as the oxygen carrier, like cobalt phthalocyanine [13], cobalt Schiff [14,15,16], and cobalt porphyrins [17,18,19,20,21,22,23,24]. They have a reversible interaction with O2, facilitating O2 transportation prior to other gases in membranes, so that the O2 separation performance is improved. Nagar et al. [13] prepared the facilitated transport membrane using cobalt phthalocyanine (CoPc) as the oxygen carrier and studied the effect of CoPc content and feed pressure on the O2/N2 separation performance. The O2 permeance and O2/N2 selectivity are up to 1.12 GPU (1 GPU = 10−6 cm3 cm−2 s−1 cmHg−1) and 8.5 at the CoPc content of 1 wt % and the feed pressure of 2 bar. Matsuoka et al. [15] fabricated two kinds of liquid membranes with N,N′-bis(salicylidene)ethylenediamine cobalt-based ionic liquid as the oxygen carrier. At a low feed pressure of 1 kPa, the O2/N2 separation performance overcomes the 2008 Robeson upper bound. Cobalt porphyrins were also applied as oxygen carriers owing to their high O2 affinity, easy preparation, and high stability. Yang et al. [19] investigated the effect of cobalt porphyrins with different substituents and axial ligands on the O2 permeability and O2/N2 ideal selectivity. The results showed the cobalt porphyrin containing an electron-accepting substituent (–Cl) and imidazole as the ligand could increase the O2/N2 selectivity of the ethyl cellulose membrane. The O2 permeability and O2/N2 selectivity are 12.39 barrer and 4.44, respectively. This is due to the electron-accepting substituent (–Cl) decreasing the electron density at the center cobalt ion via electron-inductive effects and decreasing the oxygen-binding rate, hence increasing the O2/N2 selectivity [20]. Shinohara et al. [21] prepared cobalt tetraazaporphyrin with a polymeric imidazole ligand and investigated its O2 separation performance, similarly showing that the low electron density at the cobalt ion leads to low oxygen-binding affinity and enhances the oxygen-releasing rate constant to elevate the O2 separation performance. The O2/N2 selectivity is up to 28 with a relatively low O2 permeability of 2.9 barrer. Shoji et al. [22] developed cobalt porphyrin-Nafion membranes and studied the O2/N2 separation performance. The results showed that the membrane containing cobalt porphyrin with the electron-accepting group –F (meso-tetrakis(pentafluorophenyl)porpyrinatocobalt, CoFPP) has a higher O2/N2 selectivity than that including meso-tetraphenylporphyrinatocobalt (CoTPP) as the carrier because the CoFPP has a lower oxygen-binding affinity than the CoTPP. Choi et al. [24] investigated the O2/N2 separation performance of the poly(n-butyl methacrylate)-cobalt tetraphenylporphyrin composite hollow fiber membrane and the O2 permeability and O2/N2 selectivity are ≈5.2 barrer and 3.2, respectively. However, both the metalloporphyrin and polymer are solids. Their surface compatibility is still challenged and improved. Obviously, good compatibility is beneficial to the dispersion of the metalloporphyrin, increasing the O2 transport efficiency and then improving the membrane separation performance.
In this work, we developed a novel thin-film composite (TFC) membrane for O2/N2 separation, which was fabricated using the cobalt porphyrin (T(p-OCH3)PPCoCl) as the oxygen carrier, Pebax-2533 as the polymer matrix, and macroporous PVDF as the support. The substitute –OCH3 connected to porphyrin was favorable for the compatibility between cobalt porphyrin and Pebax-2533. The cobalt porphyrin with –Cl as the axial ligand could decrease the electron density at the cobalt ion, and decrease the oxygen-binding affinity, hence enhance the oxygen-releasing rate to achieve the effective O2/N2 separation. The prepared TFC membranes were characterized, and the existing interaction between T(p-OCH3)PPCoCl and O2 was proved via simulation. The influence of T(p-OCH3)PPCoCl with different contents and different pressures on the O2 permeability, N2 permeability, and O2/N2 selectivity was systematically studied.

2. Materials and Methods

2.1. Materials

The PVDF support membrane with a pore size of 0.1 μm and an average thickness of 100 μm was purchased from Hangzhou Anow Microfiltration Co., Ltd. (Hangzhou, China). Pebax-2533 containing 80 wt % of poly(tetramethylene oxide) (PTMEO) and 20 wt % of nylon 12 (PA12) was provided by Arkema (Paris, France), and its structure is shown in Chart 1a. The N2 (99.999%) and O2 (99.999%) were supplied by Beijing Beiwen Gas Factory (Beijing, China). Hydrochloric acid, anhydrous methanol, and ethanol were purchased from Beijing Chemical Works (Beijing, China). o-nitrotoluene, p-anisaldehyde, propionic acid, and acetic acid were supplied by Aladdin (Shanghai, China). Pyrrole and anhydrous cobalt dichloride (CoCl2) was purchased from Sinopharm Chemical Reagent Co., Ltd. (Shanghai, China). Dimethylformamide (DMF) was provided by Xilong Scientific Co., Ltd. (Guangdong, China). Deionized water was used throughout the study.

2.2. Synthesis of Cobalt Porphyrin

Tetra(p-methoxylphenyl)porphyrin (T(p-OCH3)PP) was prepared according to the literature [25,26] with some revisions. In a three-necked flask, propionic acid (20 mL), acetic acid (10 mL), and o-nitrotoluene (10 mL) were added. The mixture was heated to reflux, and then p-anisaldehyde (10 mmol) was added into the refluxing mixture and stirred for 5–6 min. Pyrrole (10 mmol) dissolved in o-nitrotoluene (10 mL) was added dropwise and reacted for 1 h. The mixture was allowed to cool to 60 °C, and then 30 mL of methanol was added slowly and set aside for recrystallization. The blue crystals were filtered and washed three times with water and methanol. The resulting T(p-OCH3)PP product (0.34 g, 18.5% yield) was obtained and dried at 60 °C under vacuum for 8 h. 1H NMR (600 MHz, CDCl3) δ (ppm): −2.75 (s, 2H); 4.10 (s, 12H); 7.28 (d, J = 8.4 Hz, 8H); 8.12 (d, J = 8.4 Hz, 8H); 8.86 (s, 8H).
Tetra(p-methoxylphenyl)porphyrin cobalt chloride (T(p-OCH3)PPCoCl) (Chart 1b) was synthesized according to the literature [27]. T(p-OCH3)PP (147 mg, 0.2 mmol), DMF(30 mL) and acetic acid (3 mL) were added into a three-necked flask and heated to reflux for 30 min. Then, CoCl2 (156 mg, 1.2 mmol) was added with five portions and reacted for 5 h. After the mixture was cooled down to room temperature, hydrochloric acid aqueous solution (40 mL, ≈19 wt %) was poured into the flask and held overnight for recrystallization. The crystals were filtered, washed thoroughly with hydrochloric acid aqueous solution (200 mL, ≈8 wt %), and dried at 60 °C under vacuum for 8 h to obtain purple crystals of T(p-OCH3)PPCoCl (160 mg, yield 97%).

2.3. Membrane Preparation

Free-standing Pebax-2533 membrane and T(p-OCH3)PPCoCl/Pebax-2533 mixed matrix membranes (MMMs) were prepared using a solution-casting method. Pebax-2533 pellets were dissolved in ethanol (10 wt %) with magnetic stirring at 80 °C for 3 h. A predetermined amount of T(p-OCH3)PPCoCl was then added and stirred at 40 °C for 2 h. After that, the solution was cast onto a glass dish and dried at room temperature for 24 h to form a sheet of membrane, which was further dried under vacuum at 60 °C for 8 h.
TFC membranes of T(p-OCH3)PPCoCl/Pebax-2533 on PVDF supports were prepared using a dip-coating method. Pre-weighed amounts of Pebax-2533 pellets were dissolved in hot ethanol at 80 °C to obtain a homogeneous solution (2 wt %). Then, T(p-OCH3)PPCoCl was added and the mixture was stirred continuously at 40 °C until it became homogeneous. The solution was degassed and poured into a glass cell. After that, the prefixed substrate PVDF on a glass pane was vertically immersed into the glass cell with the T(p-OCH3)PPCoCl/Pebax-2533 solution and then dried at ambient temperature for 2 h. Finally, the composite membranes were dried in a vacuum oven at 60 °C for 8 h to remove any solvent residue.

2.4. Characterization Methods

Ultraviolet-visible (UV-Vis) spectra of T(p-OCH3)PP and T(p-OCH3)PPCoCl were recorded in toluene on a Shimadzu UV-2550 spectrophotometer (Shimadzu Corporation, Kyoto, Japan) in the range of 350–680 nm. The Fourier transform infrared (FTIR) spectrum of T(p-OCH3)PPCoCl and the attenuated total reflectance Fourier transform infrared (ATR-FTIR) spectra of Pebax-2533 and MMMs were obtained using a Thermo Nicolet 380 spectrometer (Thermo Electron Corporation, Madison, WI, USA) in the range of 650–4000 cm−1 under ambient conditions. Wide angle X-ray diffraction (WAXRD) patterns of the MMMs were measured using a Smartlab (9 kW) diffractometer (Rigaku Corporation, Tokyo, Japan) at a scan rate of 15° min−1; the d-spacing values were calculated based on the diffraction peak maxima using Bragg’s equation. The surface and cross-sectional morphologies of the TFC membranes were observed using SU8020 scanning electron microscopy (SEM) (Hitachi High-Technologies Corporation, Tokyo, Japan). Before scanning, the membranes were fractured in liquid nitrogen and sputtered with gold.
The O2 and N2 permeation tests were carried out at ambient temperature using the standard constant-pressure, variable-volume method [28]. The feed pressure varied from 0.035 to 0.8 MPa in gauge mode, and the permeate pressure was kept at atmospheric pressure. Gas permeability was calculated using the following equation:
P = Q l t A ( p 1 − p 2 )
where P is the gas permeability (barrer, 1 barrer = 10−10 (cm3 (STP) cm cm−2 s−1 cmHg−1), Q is the volume of permeated gas (cm3 (STP)), l is the film thickness (cm), t is the permeation time (s), A is the effective membrane area (cm2), and p 1 and p 2 are the upstream and permeate side pressures (cmHg), respectively. The ideal selectivity ( S ) is defined as the ratio of the pure gas permeability of the faster gas O2 ( P A ) over that of the slower permeant N2 ( P B ):
S = P A P B

2.5. Molecular Modeling

Molecular geometries (O2, N2, and T(p-OCH3)PPCoCl) were optimized using density functional theory (DFT) calculations with Gaussian 09 software (Gaussian, Inc., Wallingford, CT, USA) [29]. The formation of complexes between T(p-OCH3)PPCoCl and N2/O2 with several different structures were fabricated by locating N2 or O2 at different positions around T(p-OCH3)PPCoCl, and the energy minimizations of all complexes were implemented to determine the optimized geometry. All of the optimizations were explored at the B3LYP/6-311G (d, p) level. The interaction energies between T(p-OCH3)PPCoCl and N2/O2 were calculated at the same level.

3. Results and Discussion

3.1. Synthesis and Characterization of T(p-OCH3)PPCoCl

T(p-OCH3)PP was prepared in a mixed solvent of propionic acid, acetic acid, and o-nitrotoluene under an air atmosphere. Propionic acid and acetic acid were used as catalysts for the condensation of pyrrole and p-anisaldehyde to obtain porphyrinogen, which was further oxidized by the oxygen (air) and o-nitrotoluene to produce T(p-OCH3)PP with a yield of 18.5%. Compared with other metalloporphyrins, cobalt porphyrin has a higher stability [30]. Therefore, T(p-OCH3)PPCoCl was used as the O2 carrier and prepared in DMF with a high yield (97%). The obtained T(p-OCH3)PP and T(p-OCH3)PPCoCl were characterized using UV-vis and the spectra are shown in Figure 1. T(p-OCH3)PP exhibited a characteristic major Soret band at 422.8 nm owing to the π→π* transition, and four visible Q bands at 518.2, 554.7, 595.2, and 653.3 nm. The Soret band of T(p-OCH3)PPCoCl shifted to a longer wavelength of 441.7 nm and two Q bands emerged at 556.8 nm and 596.1 nm. The decreased amount of Q bands can be ascribed the metalation of T(p-OCH3)PP, which increased the molecular symmetry [31].

3.2. Membranes Properties and Characterizations

The interaction between Pebax-2533 matrix and T(p-OCH3)PPCoCl was investigated using FTIR, and the spectra of T(p-OCH3)PPCoCl, neat Pebax-2533 membrane, and T(p-OCH3)PPCoCl/Pebax-2533 MMMs are given in Figure 2. The absorption peaks at 2834.0, 1606.2, 1351.2, 1248.8, and 1001.7 cm−1 for T(p-OCH3)PPCoCl were assigned to C–H, C=C, C=N, –C–O–C, and Co–N stretching vibrations, respectively. The spectrum of neat Pebax-2533 membrane was in accordance with the literature [32,33], in which the bands at 3307.9, 1734.7, 1638.2, and 1104.0 cm−1 represent the N–H, C=O, H–N–C=O, and C–O stretching, respectively. The peak at 1248.8 cm−1 corresponds to the –C–O–C stretching vibration, which showed an increasing intensity with the increasing of the T(p-OCH3)PPCoCl content in the MMMs, as expected. More importantly, the –C–O–C stretching vibration in T(p-OCH3)PPCoCl shifted to a longer wavelength from 1248.8 to 1243.9 cm−1 in MMMs and the N–H stretching vibration in Pebax-2533 similarly shifted to a longer wavelength from 3307.9 to 3296.8 cm−1, confirming substantial hydrogen bonding was formed in the composite membranes [34]. The formation of hydrogen bonding could improve the affinity between T(p-OCH3)PPCoCl and Pebax-2533, thus avoiding interfacial defects.
To investigate the effect of T(p-OCH3)PPCoCl on the chain packing structure of Pebax-2533, XRD patterns of the Pebax-2533 membrane, 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 MMM and 2 wt % T(p-OCH3)PPCoCl/Pebax-2533 MMM were measured, as shown in Figure 3. The neat Pebax-2533 membrane had a broad peak located at 2θ = 19.8°, which corresponds to a d-spacing value of 4.5 Å. The broad halo was identified as the inter-chain distance of amorphous regions [35,36,37]. Adding T(p-OCH3)PPCoCl into Pebax-2533 matrix did not change the polymer chain packing structure, as evidenced in Figure 3, where the d-spacing values of the MMMs were the same as that of the pure Pebax-2533 membrane. No crystal peak of T(p-OCH3)PPCoCl was observed in the WAXD patterns. This could have originated from a small weight fraction of the T(p-OCH3)PPCoCl and suggests a good compatibility in the T(p-OCH3)PPCoCl/Pebax-2533 composite membranes.
Figure 4 exhibits the surface and cross-sectional morphologies of the Pebax-2533 membrane and 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane. SEM images display homogeneous surfaces, and the cross-sectional view (Figure 4c) of Pebax-2533 shows two layers, i.e., the top selective layer with a film thickness of 1 μm and the PVDF substrate. As shown in Figure 4b,d, no particulate clusters were observed, indicating that T(p-OCH3)PPCoCl was well dispersed at the molecular level in the Pebax-2533 matrix without obvious agglomerations.

3.3. Molecular Modeling of O2/N2 and T(p-OCH3)PPCoCl Interactions

The optimized structures of the T(p-OCH3)PPCoCl and the interaction between T(p-OCH3)PPCoCl and gas molecules were studied using molecular modeling, and the results are shown in Figure 5. T(p-OCH3)PPCoCl exhibited a three-dimensional and distorted structure (Figure 5a), and it may have increased the fractional free volume and gas permeability of the membranes by disrupting the polymer chain packing. In the T(p-OCH3)PPCoCl–N2 complex (Figure 5b), the distance between 97Co and 120N was 3.25 Å, and there was no obvious bond, confirming there was no interaction between T(p-OCH3)PPCoCl and N2. However, in the T(p-OCH3)PPCoCl–O2 complex (Figure 5c), O2 interacted with the central cobalt ion of T(p-OCH3)PPCoCl to form a six-coordinate complex (Figure 5c). The distance of 97Co–119O was 1.89 Å, which is the same as the length of the reported Co–O coordinate bond [38], showing the coordinate bond was formed between 97Co and 119O. It indicates there was an interaction between T(p-OCH3)PPCoCl and O2. At the same time, the distance of 97Co–118Cl (2.31 Å) in the T(p-OCH3)PPCoCl–O2 complex was longer than that (2.20 Å) in T(p-OCH3)PPCoCl and shows the strength of the 97Co–118Cl bond decreased during the T(p-OCH3)PPCoCl–O2 complex formation. Their interaction energies between T(p-OCH3)PPCoCl and N2 or O2 estimated using quantum chemical calculations were −1.03 kcal/mol and −23.54 kcal/mol, respectively. It shows the interaction between T(p-OCH3)PPCoCl and O2 was higher than that between T(p-OCH3)PPCoCl and N2 and they may be reversible chemical and physical interactions separately. The reversible interaction makes T(p-OCH3)PPCoCl selectively adsorb oxygen and facilitate its transport in the membrane.

3.4. Gas Permeation Properties

The influence of the T(p-OCH3)PPCoCl content on O2 and N2 permeability and O2/N2 selectivity were systematically investigated. It can be seen from Figure 6a that the N2 permeability increased with the increasing T(p-OCH3)PPCoCl content. Given that there was almost no interaction between N2 and T(p-OCH3)PPCoCl (interaction energy of −1.03 kcal/mol), the increase of the N2 permeability was mainly due to the increase of the free volume resulting from adding the twisted T(p-OCH3)PPCoCl into the membrane. However, the O2 permeability first increased and then decreased with the increasing T(p-OCH3)PPCoCl content. The O2 permeability of the T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane reached a maximum value of 9.7 barrer at 1.2 wt % T(p-OCH3)PPCoCl content, which is about 2.6 times that of a pure Pebax-2533 membrane. The suitable interaction energy of −23.54 kcal/mol between O2 and T(p-OCH3)PPCoCl made T(p-OCH3)PPCoCl selectively adsorb O2 and then release O2 quickly, thus facilitating the O2 transport in the membrane and enhancing the O2 separation performance. When the T(p-OCH3)PPCoCl content was between 0–1.2 wt %, there were more T(p-OCH3)PPCoCl molecules to interact with O2 and facilitate its transport in the membrane with the increasing of T(p-OCH3)PPCoCl content. Meanwhile, the addition of T(p-OCH3)PPCoCl increased the free volume of the membranes. These led to an increase of the O2 permeability. However, when further increasing the T(p-OCH3)PPCoCl content, the O2 permeability decreased, probably owing to the aggregation of T(p-OCH3)PPCoCl particles. The O2/N2 selectivity also increased initially and then decreased with the T(p-OCH3)PPCoCl content increase (Figure 6b). The T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane with the T(p-OCH3)PPCoCl content of 0.6 wt % exhibited the maximum O2/N2 selectivity of 4.2 and a relatively high O2 permeability of 8.0 barrer.
Gas feed pressure also has a great influence on the O2 separation performance, and the results of the investigation is shown in Figure 7a,b. The O2 and N2 permeability of the membrane without T(p-OCH3)PPCoCl almost remained constant when varying the feed pressure, indicating the change of pressure had no obvious influence. For the TFC membrane containing 0.6 wt % T(p-OCH3)PPCoCl, the N2 permeability increased slightly with the increasing feed pressure. The O2 permeability also remained constant when the feed pressure was higher than 0.1 MPa, but interestingly, the O2 permeability increased significantly from 8.0 barrer to 12.2 barrer, and the O2/N2 selectivity increased from 4.2 to 7.6 by lowering the feed pressure from 0.1 MPa to 0.035 MPa. This indicates that the lower pressure was beneficial for O2 separation because the chemical interaction between O2 and the carrier was predominant at low feed pressure [39], hence promoting the oxygen transport by T(p-OCH3)PPCoCl.
The O2/N2 separation performances of the T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane were plotted against the 2008 Robeson upper bound, as shown in Figure 8. Compared with the membrane without T(p-OCH3)PPCoCl, the adding of T(p-OCH3)PPCoCl could enhance the separation performance mainly because T(p-OCH3)PPCoCl could efficiently facilitate O2 transport in the membrane, as well as the non-planar T(p-OCH3)PPCoCl increasing the gas permeability by increasing the fractional free volume. As the feed pressure was reduced, the separation performance was promoted gradually. The O2 permeability and O2/N2 selectivity were 12.2 barrer and 7.6, respectively, at 0.035 MPa, which is near the 2008 Robeson upper bound. For the facilitated membranes, lowering the feed pressure could enhance the separation performance. However, the separation performance of the 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane could reach the 2008 upper bound at a feed pressure of 35 kPa, which is higher than the feed pressures (<20 kPa) of the reported lectures [15,19,21,22,23]. It shows the separation performance of the membrane could more easily reach the upper bound than the reported membranes by reducing the feed pressure. The separation performances of the reported membranes are presented in Table 1 for comparison. The data shows the 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane had satisfactory separation performance. Its O2/N2 selectivity was lower than only that of the 1 wt % CoPc/Pebax-1657 membrane and 20 wt % CoFPP Nafion membrane, but its O2 permeance was much higher than theirs. Thus, the T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane is a promising candidate for O2/N2 separation.

4. Conclusions

T(p-OCH3)PPCoCl/Pebax-2533 TFC membranes with a thin and defect-free active layer were prepared. The T(p-OCH3)PPCoCl and Pebax-2533 had good compatibility due to the formation of the hydrogen bond, improving the dispersion of the T(p-OCH3)PPCoCl in Pebax-2533. T(p-OCH3)PPCoCl as an oxygen carrier could not only facilitate oxygen transport due to the reversible interaction between T(p-OCH3)PPCoCl and O2, but also increase the membrane free volume, enhancing the O2 and N2 permeability and O2/N2 selectivity. The T(p-OCH3)PPCoCl content and feed pressure had a great influence on membrane separation performance. The 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 TFC membrane exhibited a better O2 permeability of 8.0 barrer and a O2/N2 selectivity of 4.2 than that of the TFC membrane without T(p-OCH3)PPCoCl (3.7 barrer and 2.6) at 0.1 MPa. Decreasing the feed pressure was beneficial for the O2 separation in the membrane. The O2 permeability and O2/N2 selectivity significantly increased to 12.2 barrer and 7.6 at 0.035 MPa, which is up to the 2008 Robeson upper bound.

Author Contributions

Conceptualization, S.Z. and X.Z.; Investigation, J.H.; Methodology, J.H. and B.Y.; Software, Y.B.; Writing—original draft, J.H.; Writing—review and editing, L.B., S.L., S.Z., H.G., Y.N., and X.J.

Funding

This work was supported by the National Key R&D Program of China (2017YFB0603401-03), the National Natural Science Foundation of China (21978306, 21425625, 51574215), the Beijing Hundreds of Leading Talents Training Project of Science and Technology (Z171100001117154), the State Key Laboratory of Separation Membranes and Membrane Processes (Tianjin Polytechnic University) (M2-201808), and the Zhengzhou High Level Talent (No. 20180200029).

Conflicts of Interest

The authors declare that they have no conflict of interest.

Abbreviations

Pebaxpoly(amide-12-b-ethylene oxide)
T(p-OCH3)PPCoCltetra(p-methoxylphenyl)porphyrin cobalt chloride
PVDFpolyvinylidene fluoride
TFCthin film composite
CoPccobalt phthalocyanine
CoFPPmeso-tetrakis(pentafluorophenyl)porpyrinatocobalt
CoTPPmeso-tetraphenylporphyrinatocobalt
T(p-OCH3)PPtetra(p-methoxylphenyl)porphyrin
MMMsmixed matrix membranes
MgPcmagnesium phathalocyanine
PEIpolyetherimide
PUpolyurethane
SiO2–PVP–salcomineSiO2–poly(N-vinylpyrrolidone)–(N,N-disalicylideneethylenediaminato)cobalt
[P66614]2[Co(salen)(N-mGly)(Tf2N)][trihexyl(tetradecyl)phosphonium]2[N,N-bis(salicylidene)ethylenediamine cobalt(N-methylglycinate)(bis(trifluoromethanesulfonyl)imid)]
[P66614]2[Co(salen)(N-mGly)2][trihexyl(tetradecyl)phosphonium]2[N,N-bis(salicylidene)ethylenediamine cobalt(N-methylglycinate)2]
ECethyl cellulose
CoT(2-Cl)PPcobalt(II) meso-tetrakis(2-chlorophenyl) porphyrin
Imimidazole
OImpoly[(octyl methacrylate)-co-vinylimidazole]
CoTAPcobalt tetra-tert-butyltetraazaporphyrin
CoPac5-(4-benzylacetoacetate)-10, 15, 20-triphenylcobaltporphyrin
PTApentaerythritol tetraacrylate

References

  1. Cardona, C.A.; Amell, A.A. Laminar burning velocity and interchangeability analysis of biogas/C3H8/H2 with normal and oxygen-enriched air. Int. J. Hydrogen Energy 2013, 38, 7994–8001. [Google Scholar] [CrossRef]
  2. Caro, J. Oxygen-Enriched Air (OEA) Production by Membrane Reactors. In Encyclopedia of Membranes; Drioli, E., Giorno, L., Eds.; Springer: Heidelberg, Berlin, Germany, 2016; pp. 1446–1447. ISBN 978-3-662-44324-8. [Google Scholar]
  3. Chong, K.C.; Lai, S.O.; Lau, W.J.; Thiam, H.S.; Ismail, A.F.; Zulhairun, A.K. Fabrication and Characterization of Polysulfone Membranes Coated with Polydimethysiloxane for Oxygen Enrichment. Aerosol Air Qual. Res. 2017, 17, 2735–2742. [Google Scholar] [CrossRef]
  4. Hemmati-Sarapardeh, A.; Mohagheghian, E. Modeling interfacial tension and minimum miscibility pressure in paraffin-nitrogen systems: Application to gas injection processes. Fuel 2017, 205, 80–89. [Google Scholar] [CrossRef]
  5. Frank, M.; Drikakis, D. Draining Water from Aircraft Fuel Using Nitrogen Enriched Air. Energies 2018, 11, 908. [Google Scholar] [CrossRef]
  6. Wang, Y.; Yang, R.T. Chemical Liquid Deposition Modified 4A Zeolite as a Size-Selective Adsorbent for Methane Upgrading, CO2 Capture and Air Separation. ACS Sustain. Chem. Eng. 2019, 7, 3301–3308. [Google Scholar] [CrossRef]
  7. Belaissaoui, B.; Le Moullec, Y.; Hagi, H.; Favre, E. Energy efficiency of oxygen enriched air production technologies: Cryogeny vs membranes. Sep. Purif. Technol. 2014, 125, 142–150. [Google Scholar] [CrossRef]
  8. Hu, T.; Zhou, H.; Peng, H.; Jiang, H. Nitrogen Production by Efficiently Removing Oxygen From Air Using a Perovskite Hollow-Fiber Membrane With Porous Catalytic Layer. Front. Chem. 2018, 6, 329. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  9. Chong, K.C.; Lai, S.O.; Thiam, H.S.; Teoh, H.C.; Heng, S.L. Recent progress of oxygen nitrogen separation using membrane technology. J. Eng. Sci. Technol. 2016, 11, 1016–1030. [Google Scholar]
  10. Wang, H.H.; Werth, S.; Schiestel, T.; Caro, A. Perovskite hollow-fiber membranes for the production of oxygen-enriched air. Angew. Chem. Int. Ed. 2005, 44, 6906–6909. [Google Scholar] [CrossRef]
  11. Dong, G.; Zhang, X.; Zhang, Y.; Tsuru, T. Enhanced Permeation through CO2-Stable Dual-Inorganic Composite Membranes with Tunable Nanoarchitectured Channels. ACS Sustain. Chem. Eng. 2018, 6, 8515–8524. [Google Scholar] [CrossRef]
  12. Robeson, L.M. The upper bound revisited. J. Membr. Sci. 2008, 320, 390–400. [Google Scholar] [CrossRef]
  13. Nagar, H.; Vadthya, P.; Prasad, N.S.; Sridhar, S. Air separation by facilitated transport of oxygen through a Pebax membrane incorporated with a cobalt complex. RSC Adv. 2015, 5, 76190–76201. [Google Scholar] [CrossRef]
  14. Kuraoka, K.; Chujo, Y.; Yazawa, T. A novel inorganic-organic hybrid membrane for oxygen/nitrogen separation containing a cobalt(II) Schiff base complex as oxygen carrier using poly(N-vinylpyrrolidone) as mediator. Chem. Commun. 2000, 24, 2477–2478. [Google Scholar] [CrossRef]
  15. Matsuoka, A.; Kamio, E.; Mochida, T.; Matsuyama, H. Facilitated O2 transport membrane containing Co(II)-salen complex-based ionic liquid as O2 carrier. J. Membr. Sci. 2017, 541, 393–402. [Google Scholar] [CrossRef]
  16. Ruaan, R.C.; Chen, S.H.; Lai, J.Y. Oxygen/nitrogen separation by polycarbonate/Co(SalPr) complex membranes. J. Membr. Sci. 1997, 135, 9–18. [Google Scholar] [CrossRef]
  17. Nishide, H.; Ohyanagi, M.; Okada, O.; Tsuchida, E. Highly Selective Transport of Molecular Oxygen in a Polymer Containing a Cobalt Porphyrin Complex as a Fixed Carrier. Macromolecules 1986, 19, 494–496. [Google Scholar] [CrossRef]
  18. Nishide, H.; Ohyanagi, M.; Okada, O.; Tsuchida, E. Dual-Mode Transport of Molecular Oxygen in a Membrane Containing a Cobalt Porphyrin Complex as a Fixed Carrier. Macromolecules 1987, 20, 417–422. [Google Scholar] [CrossRef]
  19. Yang, J.P.; Huang, P.C. Facilitated transport of oxygen in ethyl cellulose membranes containing cobalt porphyrins as oxygen carriers. J. Appl. Polym. Sci. 2000, 77, 484–488. [Google Scholar] [CrossRef]
  20. Yang, J.P.; Huang, P.C. A study of cobalt(II) porphyrins on their oxygen-binding behaviors and oxygen-facilitated transport properties in polymeric membranes. Chem. Mater. 2000, 12, 2693–2697. [Google Scholar] [CrossRef]
  21. Shinohara, H.; Shibata, H.; Wohrle, D.; Nishide, H. Reversible oxygen binding to the polymeric cobalt tetraazaporphyrin complex and oxygen-facilitated transport through its membrane. Macromol. Rapid Commun. 2005, 26, 467–470. [Google Scholar] [CrossRef]
  22. Shoji, M.; Oyaizu, K.; Nishide, H. Facilitated oxygen transport through a Nafion membrane containing cobaltporphyrin as a fixed oxygen carrier. Polymer 2008, 49, 5659–5664. [Google Scholar] [CrossRef]
  23. Chikushi, N.; Ohara, E.; Hisama, A.; Nishide, H. Porphyrin Network Polymers Prepared via a Click Reaction and Facilitated Oxygen Permeation Through Their Membranes. Macromol. Rapid Commun. 2014, 35, 976–980. [Google Scholar] [CrossRef] [PubMed]
  24. Choi, W.; Ingole, P.G.; Li, H.; Kim, J.H.; Lee, H.K.; Baek, I.H. Preparation of facilitated transport hollow fiber membrane for gas separation using cobalt tetraphenylporphyrin complex as a coating material. J. Clean. Prod. 2016, 133, 1008–1016. [Google Scholar] [CrossRef]
  25. Sun, Z.; She, Y.; Zhong, R. Synthesis of p-substituted tetraphenylporphyrins and corresponding ferric complexes with mixed-solvents method. Front. Chem. Eng. China 2009, 3, 457–461. [Google Scholar] [CrossRef]
  26. Momo, P.B.; Bellete, B.S.; Brocksom, T.J.; De Souza, R.O.M.A.; De Oliveira, K.T. Exploiting novel process windows for the synthesis of meso-substituted porphyrins under continuous flow conditions. RSC Adv. 2015, 5, 84350–84355. [Google Scholar] [CrossRef]
  27. Kumar, A.; Maji, S.; Dubey, P.; Abhilash, G.J.; Pandey, S.; Sarkar, S. One-pot general synthesis of metalloporphyrins. Tetrahedron Lett. 2007, 48, 7287–7290. [Google Scholar] [CrossRef]
  28. Bhavsar, R.S.; Mitra, T.; Adams, D.J.; Cooper, A.I.; Budd, P.M. Ultrahigh-permeance PIM-1 based thin film nanocomposite membranes on PAN supports for CO2 separation. J. Membr. Sci. 2018, 564, 878–886. [Google Scholar] [CrossRef]
  29. Frisch, M.J.; Trucks, G.W.; Schlegel, H.B.; Scuseria, G.E.; Robb, M.A.; Cheeseman, J.R.; Scalmani, G.; Barone, V.; Mennucci, B.; Petersson, G.A.; et al. Gaussian 09, Revision D. 01, Gaussian, Inc., Wallingford CT, 2013 Search PubMed;(b) AD Becke. J. Chem. Phys. 1993, 5648, 785–789. [Google Scholar]
  30. Li, G.Q.; Govind, R. Separation of Oxygen from Air Using Coordination Complexes: A Review. Ind. Eng. Chem. Res. 1994, 33, 755–783. [Google Scholar] [CrossRef]
  31. Chen, W.T.; El-Khouly, M.E.; Fukuzumi, S. Saddle Distortion of a Sterically Unhindered Porphyrin Ring in a Copper Porphyrin with Electron-Donating Substituents. Inorg. Chem. 2011, 50, 671–678. [Google Scholar] [CrossRef]
  32. De Dai, Z.; Bai, L.; Hval, K.N.; Zhang, X.P.; Zhang, S.J.; Deng, L.Y. Pebax®/TSIL blend thin film composite membranes for CO2 separation. Sci. China Chem. 2016, 59, 538–546. [Google Scholar] [CrossRef]
  33. Sridhar, S.; Aminabhavi, T.M.; Mayor, S.J.; Ramakrishna, M. Permeation of carbon dioxide and methane gases through novel silver-incorporated thin film composite Pebax membranes. Ind. Eng. Chem. Res. 2007, 46, 8144–8151. [Google Scholar] [CrossRef]
  34. Wang, H.; Liu, S.; Zhao, Y.; Wang, J.; Yu, Z. Insights into the Hydrogen Bond Interactions in Deep Eutectic Solvents Composed of Choline Chloride and Polyols. ACS Sustain. Chem. Eng. 2019, 7, 7760–7767. [Google Scholar] [CrossRef]
  35. Nafisi, V.; Hagg, M.B. Development of Nanocomposite Membranes Containing Modified Si Nanoparticles in PEBAX-2533 as a Block Copolymer and 6FDA-Durene Diamine as a Glassy Polymer. ACS Appl. Mater. Interfaces 2014, 6, 15643–15652. [Google Scholar] [CrossRef] [PubMed]
  36. Nafisi, V.; Hagg, 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]
  37. Dong, L.; Zhang, C.; Bai, Y.; Shi, D.; Li, X.; Zhang, H.; Chen, M. High-Performance PEBA2533-Functional MMT Mixed Matrix Membrane Containing High-Speed Facilitated Transport Channels for CO2/N2 Separation. ACS Sustain. Chem. Eng. 2016, 4, 3486–3496. [Google Scholar] [CrossRef]
  38. Li, J.F.; Noll, B.C.; Oliver, A.G.; Scheidt, W.R. Structural Insights into Ligand Dynamics: Correlated Oxygen and Picket Motion in Oxycobalt Picket Fence Porphyrins. J. Am. Chem. Soc. 2012, 134, 10595–10606. [Google Scholar] [CrossRef] [PubMed] [Green Version]
  39. Shentu, B.Q.; Nishide, H. Facilitated oxygen transport membranes of picket-fence cobaltporphyrin complexed with various polymer matrixes. Ind. Eng. Chem. Res. 2003, 42, 5954–5958. [Google Scholar] [CrossRef]
  40. Kurdi, J.; Tremblay, A.Y. Improvement in polyetherimide gas separation membranes through the incorporation of nanostructured metal complexes. Polymer 2003, 44, 4533–4540. [Google Scholar] [CrossRef]
  41. Chen, S.H.; Yu, K.C.; Houng, S.L.; Lai, J.Y. Gas transport properties of HTPB based polyurethane/cosalen membrane. J. Memb. Sci. 2000, 173, 99–106. [Google Scholar] [CrossRef]
Membranes 09 00115 ch001 550
Chart 1. Chemical structures of Pebax-2533 (a) and T(p-OCH3)PPCoCl (b).
Chart 1. Chemical structures of Pebax-2533 (a) and T(p-OCH3)PPCoCl (b).
Membranes 09 00115 ch001
Membranes 09 00115 g001 550
Figure 1. UV-vis spectra of T(p-OCH3)PP and T(p-OCH3)PPCoCl.
Figure 1. UV-vis spectra of T(p-OCH3)PP and T(p-OCH3)PPCoCl.
Membranes 09 00115 g001
Membranes 09 00115 g002 550
Figure 2. FTIR spectra of T(p-OCH3)PPCoCl (a), Pebax-2533 membrane (b), 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (c) and 2 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (d).
Figure 2. FTIR spectra of T(p-OCH3)PPCoCl (a), Pebax-2533 membrane (b), 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (c) and 2 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (d).
Membranes 09 00115 g002
Membranes 09 00115 g003 550
Figure 3. XRD spectra of Pebax-2533 membrane (a), 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (b), and 2 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (c).
Figure 3. XRD spectra of Pebax-2533 membrane (a), 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (b), and 2 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane (c).
Membranes 09 00115 g003
Membranes 09 00115 g004 550
Figure 4. The surface SEM images of (a) Pebax-2533 membrane and (b) 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane, and the cross-section SEM images of (c) Pebax-2533 membrane and (d) 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane.
Figure 4. The surface SEM images of (a) Pebax-2533 membrane and (b) 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane, and the cross-section SEM images of (c) Pebax-2533 membrane and (d) 0.6 wt % T(p-OCH3)PPCoCl/Pebax-2533 membrane.
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Membranes 09 00115 g005 550
Figure 5. Optimized structures of (a) T(p-OCH3)PPCoCl, (b) T(p-OCH3)PPCoCl–N2 complex, and (c) T(p-OCH3)PPCoCl–O2 complex at the B3LYP/6-311G (d, p) level.
Figure 5. Optimized structures of (a) T(p-OCH3)PPCoCl, (b) T(p-OCH3)PPCoCl–N2 complex, and (c) T(p-OCH3)PPCoCl–O2 complex at the B3LYP/6-311G (d, p) level.
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Membranes 09 00115 g006 550
Figure 6. Effect of T(p-OCH3)PPCoCl content on gas permeability (a) and O2/N2 selectivity (b).
Figure 6. Effect of T(p-OCH3)PPCoCl content on gas permeability (a) and O2/N2 selectivity (b).
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Membranes 09 00115 g007 550
Figure 7. Effect of the feed pressure on gas permeability (a) and O2/N2 selectivity (b).
Figure 7. Effect of the feed pressure on gas permeability (a) and O2/N2 selectivity (b).
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Membranes 09 00115 g008 550
Figure 8. Performance comparison with the Robeson upper bound.
Figure 8. Performance comparison with the Robeson upper bound.
Membranes 09 00115 g008
Table
Table 1. Comparison of the separation performance of the reported membranes with this work.
Table 1. Comparison of the separation performance of the reported membranes with this work.
MembraneP (bar)T (°C)SO2/N2PO2 (barrer) aRef.
1–15 wt % MgPc/PEI12.825≈2.3–5.4≈0.42–0.13 GPU b[40]
1–15 wt % CoPc/PEI12.825≈4.8–1.9≈0.25–1.13 GPU[40]
1 wt % cosalen/PU15–35≈4.2–3.0≈4.2–13.2[41]
20 wt % CoFPP/Nafion1–225≈14.2–2.0≈2.2–0.3[22]
SiO2–PVP–salcomine-25–1501.4–6.10.35–1.48 GPU[14]
1 wt % CoPc/Pebax-16572–825≈8.5–5.5≈1.12–0.93 GPU[13]
0.6 wt % T(p-OCH3)PPCoCl/Pebax-25330.35–8187.6–2.212.2–6.3This study
a 1 barrer = 10−10 cm3 cm cm−2 s−1 cmHg−1; b 1 GPU = 10−6 cm3 cm−2 s−1 cmHg−1 = 3.38 × 10−10 mol m−2 s−1 Pa−1.

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MDPI and ACS Style

Han, J.; Bai, L.; Yang, B.; Bai, Y.; Luo, S.; Zeng, S.; Gao, H.; Nie, Y.; Ji, X.; Zhang, S.; et al. Highly Selective Oxygen/Nitrogen Separation Membrane Engineered Using a Porphyrin-Based Oxygen Carrier. Membranes 2019, 9, 115. https://doi.org/10.3390/membranes9090115

AMA Style

Han J, Bai L, Yang B, Bai Y, Luo S, Zeng S, Gao H, Nie Y, Ji X, Zhang S, et al. Highly Selective Oxygen/Nitrogen Separation Membrane Engineered Using a Porphyrin-Based Oxygen Carrier. Membranes. 2019; 9(9):115. https://doi.org/10.3390/membranes9090115

Chicago/Turabian Style

Han, Jiuli, Lu Bai, Bingbing Yang, Yinge Bai, Shuangjiang Luo, Shaojuan Zeng, Hongshuai Gao, Yi Nie, Xiaoyan Ji, Suojiang Zhang, and et al. 2019. "Highly Selective Oxygen/Nitrogen Separation Membrane Engineered Using a Porphyrin-Based Oxygen Carrier" Membranes 9, no. 9: 115. https://doi.org/10.3390/membranes9090115

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