# Fabrication of Functionalized MOFs Incorporated Mixed Matrix Hollow Fiber Membrane for Gas Separation

Authors: Haitao Zhu; Xingming Jie; Yiming Cao
Journal: Journal of Chemistry
 (2017)

---

## Abstract

The metal-organic framework (MOFs) of MIL-53 was functionalized by aminosilane grafting and then incorporated into Ultem®1000 polymer matrix to fabricate mixed matrix hollow fiber membrane (MMHFM) with high separation performance. SEM, XRD, and TGA were performed to characterize the functionalized MIL-53 and prepared MMHFM. The filler particles were embedded in membrane successfully and dispersed well in the polymer matrix. The incorporation of MOFs endowed MMHFM better thermal stability. Moreover, effects of solvent ratio in spinning dope, spinning condition, and testing temperature on gas separation performance of MMHFM were investigated. By optimizing dope composition, air gap distance, and bore fluid composition, MMHFM containing functionalized MIL-53 achieved excellent gas permeance and CO2/N2 selectivity. The CO2 permeance increased from 12.2 GPU for pure Ultem HFM to 30.9 GPU and the ideal CO2/N2 selectivity was enhanced from 25.4 to 34.7 simultaneously. Additionally, gas permeance increased but the selectivity decreased with the temperature increase, which followed the solution-diffusion based transport mechanism.


---

## Body

## 1. Introduction

Membrane based gas separation and purification hold promise as energy-efficient technology if compared with traditional methods such as adsorption and cryogenic distillation [1–4]. However, the permeability-selectivity trade-off described as Robeson upper bound restricted gas separation performance of polymeric membranes [5]. Several solutions have been proposed in past decades to further improve membrane performance. One of the most effective routes to enhance the separation performance is fabrication of mixed matrix membrane (MMM) that combines inorganic materials with polymer matrix [6, 7]. Regarding the filler materials, metal-organic frameworks (MOFs) are a satisfactory alternative to improve the permeation properties of membranes because of its large surface area, high porosity, adsorption capacity, and good compatibility [8–10].Over the past few years, various MOFs have been incorporated into membranes to improve gas separation performance, such as Matrimid®5218/ZIF-8 [11], PBI/ZIF-7 [12], PI/Mg2(dobdc) [13], and Ultem/ZIF-8 [14]. Appropriate structures of MOFs are efficient for gas separation application as previous references reported [15–19]. Couck et al. [20] revealed that the amino-functionalized MOFs NH2-MIL-53 achieved excellent performance for CO2 capture. Moreover, MMM based on NH2-MIL-53 with improved structural feature and gas separation performance was synthesized by incorporating the filler particles in polyimide matrix. The membrane containing 25 wt% MOFs loading presented a 50% increment in CO2 permeability, while retaining the separation selectivity [21]. The amino-functionalized MOFs filled MMMs have been also fabricated by Seoane et al. and the membrane performance was improved approaching the Robeson CO2/CH4 and H2/CH4 upper bound with 10 wt% MOFs loading [22]. In addition, other researchers have fabricated mixed matrix composite membrane by synthesizing MOFs continuous membrane on outer-side or inner-side of hollow fiber membrane to improve gas separation performance [23–26].However, the filler particle aggregation and interfacial isolation are the major drawbacks that hinder the development of inorganic filler based MMMs [27, 28]. As a feasible method, the certain functions on MOFs could lead to enhanced interaction with functional groups of polymer chains [28]. For example, in NH2-MIL-53 incorporated MMM, the hydrogen bonding between the sulfone group of polysulfone and amine of MOFs enhanced compatibility at the polymer/filler interface [29]. Here, the present work prepared functionalized MOFs by grafting aminosilane to improve the interfacial affinity between filler particles and polymer matrix. The –NH2 group on the functionalized MOFs could interact with carbonyl group of Ultem 1000 and the grafting alkyl chains also enhanced the adhesion with polymer matrix. Moreover, the dispersion of filler particles was uniform in the aid of silicane modification. In order to prepare asymmetric MMHFM with optimal membrane structure and remarkable separation performance, we investigated the important factors including solvent/nonsolvent ratio in spinning dope solution, spinning condition (air gap distance and bore fluid composition), and testing temperature.


## 2. Experimental

### 2.1. Materials

Ultem 1000 polymer was purchased from GE Plastics in pellet form and was dried 140°C for 12 h before use. Terephthalic acid (H2BDC) was purchased from Sinopharm Chemical Reagent Co., Ltd. 3-Aminopropyltrimethoxysilane (APTMS) was purchased from J&K Scientific Ltd., Beijing, China. N,N-dimethylformamide (DMF), Al(NO3)3·9H2O, N-methyl-2-pyrrolidone (NMP), anhydrous ethanol (EtOH), n-hexane, petroleum ether, and aqueous ammonia (25 wt%) were purchased from Kemiou Chemical Reagent Co., Ltd., Tianjin, China. Polydimethylsiloxane (PDMS, Sylgard 184) was produced by Dow Chemicals.


### 2.2. Synthesis of MIL-53

MIL-53 was synthesized by the solvothermal method [30, 31]. First, Al(NO3)3·9H2O (4.22 g) and H2BDC (1.245 g) were added into the mixed solvent of 20 mL of deionized water and 55 mL of DMF and magnetically stirred for 40 min. Then the solution was transferred into a Teflon-lined steel autoclave and heated in an air oven at 150°C for 48 h. The product was centrifuged and washed with deionized water three times, followed by immersing in DMF for 8 h. Afterward, the white powder was filtered from DMF and dried in an air oven for 12 h at 150°C. Finally, the fine powdered MIL-53 was further activated at 180°C under vacuum for 12 h.


### 2.3. Functionalization of MIL-53

MIL-53 particles (2.0 g) were dispersed in the mixed solvent of 2.6 g of deionized water, 60 mL of EtOH, and 1.36 g of aqueous ammonia. The suspension was stirred and sonicated in a round-bottomed flask at 60°C for 2 h. Then 1.44 g of APTMS was added dropwise into the mixture under stirring. The suspension reacted at room temperature for 12 h and then was centrifuged to obtain the modified product and washed with EtOH at least three times to remove residual APTMS. Finally, the aminosilane modified MIL-53 was dried under vacuum at 80°C for 24 h.


### 2.4. Mixed Matrix Hollow Fiber Membrane Preparation

#### 2.4.1. Preparation of Spinning Dope

A certain amount of functionalized MIL-53 was added to a portion of the required NMP with stirred and sonicated alternatively for 45 min to obtain a well-dispersed suspension. Then MOFs filler was primed by addition of a dilute polymer solution into the suspension to ensure better adhesion. This mixture was stirred for 3 h and sonicated for 45 min until it displayed in uniform consistency. Then a required amount of EtOH was added with the remaining NMP into the suspension. Finally, the Ultem 1000 pellet was gradually added into the mixture to increase dope viscosity. After adding all the components, the suspension was mechanically stirred at 60°C for about 12 h to fully dissolve the polymer. For comparison purposes, the pure Ultem dope solution was prepared following an identical procedure. The polymer concentration in all dope solutions kept 33 wt% and the MOFs loading kept 15 wt% which was determined by(1)MOFsloadingwt%=wt.MOFswt.MOFs+wt.polymer×100%.


#### 2.4.2. MMHFM Fabrication

Asymmetric hollow fiber membranes in this study were fabricated via the dry-wet spinning method. The homogeneous dope and bore fluid were coextruded from a spinneret after dope solution was degassed; then the nascent fiber entered a water coagulant bath with a range of spinning parameters (Table1) through the air gap distance and was wound up on a take-up drum. The spinning process was performed at 60°C and a filter was attached upstream of the spinneret to prevent impurity particles blocking the narrow spinneret orifice. Proper pressure was supplied by the nitrogen cylinder to maintain a constant spinning rate and a syringe pump was used to control the flow rate of bore fluid.Table 1
Detailed spinning parameters of hollow fiber membrane fabrication.
Spinning parameters Value Spinneret dimension (mm) o.d./i.d. = 0.70 : 0.35 Spinneret temperature (C°) 60 ± 2 Air gap distance (cm) 0.8–5.0 Bore fluid composition NMP : H2O = 10 wt% : 90 wt% NMP : H2O = 50 wt% : 50 wt% NMP : H2O = 90 wt% : 10 wt% Bore fluid flow rate (mL/min) 0.27 ± 0.02 External coagulant Tap water Temperature of external coagulant (C°) 18 ± 2The as-fabricated fibers were rinsed in flowing tap water for about 24 h to remove the remaining solvent. Then the fibers were exchanged by immersing in three successive aliquots of EtOH for 30 min, followed by 30 min immersion in three successive aliquots of n-hexane. Afterward, the hollow fiber membranes were dried at 70°C for 3 h.For sealing the microvoids or defects in the skin layer, each membrane module containing fibers was dip-coated by 3 wt% Sylgard 184 solution with a corresponding curing agent (10 wt% of Sylgard 184 PDMS) in petroleum ether. After coating for 30 min, the modules were placed into a 70°C oven and cured for 3 h after petroleum ether evaporation. The coated hollow fiber membranes were tested to evaluate gas permeation properties.


### 2.5. Characterizations

The morphologies of functionalized MOFs and membranes were examined by scanning electron microscopy (SEM, Zeiss Supra 55 Sapphire). MOFs particles were tested without any dispersion. The membrane samples were frozen and broken off in liquid nitrogen and then sputtered with gold before SEM testing. MOFs and hollow fiber membranes were characterized by powder X-ray diffraction (XRD) using a PANalytical Empyrean diffractometer with Cu Kα radiation (λ = 0.15406 nm). The basal spacing was calculated by the Bragg’s equation:(2)nλ=2dsin⁡θ.Thermal stability of functionalized MIL-53, pure Ultem HFM, and MMHFM were measured by thermo-gravimetric analysis (TGA) at a heating rate of 10°C/min from room temperature to 800°C under nitrogen atmosphere using a TGA instrument (Netzsch STA449F3).


### 2.6. Pure Gas Permeation Measurement

Gas permeation experiments were conducted at 35°C with a testing pressure of 0.5 MPa. The permeation flow rate was measured with soap bubble flow meter and permeance (P/l) was calculated by the following:(3)Pl=ppVPRTVmAtΔp,where pp is the pressure of the permeate side (cmHg), VP is the volume of permeate gas during the test duration (cm3), Vm is the molar volume of ideal gas at standard condition [cm3 (STP)/mol], R is the universal gas constant, T is the absolute temperature (K),A is the permeation area (cm2), t is the test duration (s), and Δp is the trans-membrane pressure difference (cmHg). The permeance (P/l) values are commonly reported in the gas permeation unit GPU, 1 GPU = 1 × 10−6 cm3 (STP)/(cm2·s·cmHg). The ideal selectivity of gases i and j is defined as follows:(4)αi/j=P/liP/lj.For each sample, at least three membrane modules were prepared and tested as our previous work [3], and the average value of testing result (with standard deviation) was used to determine the gas separation performance.


## 2.1. Materials

Ultem 1000 polymer was purchased from GE Plastics in pellet form and was dried 140°C for 12 h before use. Terephthalic acid (H2BDC) was purchased from Sinopharm Chemical Reagent Co., Ltd. 3-Aminopropyltrimethoxysilane (APTMS) was purchased from J&K Scientific Ltd., Beijing, China. N,N-dimethylformamide (DMF), Al(NO3)3·9H2O, N-methyl-2-pyrrolidone (NMP), anhydrous ethanol (EtOH), n-hexane, petroleum ether, and aqueous ammonia (25 wt%) were purchased from Kemiou Chemical Reagent Co., Ltd., Tianjin, China. Polydimethylsiloxane (PDMS, Sylgard 184) was produced by Dow Chemicals.


## 2.2. Synthesis of MIL-53

MIL-53 was synthesized by the solvothermal method [30, 31]. First, Al(NO3)3·9H2O (4.22 g) and H2BDC (1.245 g) were added into the mixed solvent of 20 mL of deionized water and 55 mL of DMF and magnetically stirred for 40 min. Then the solution was transferred into a Teflon-lined steel autoclave and heated in an air oven at 150°C for 48 h. The product was centrifuged and washed with deionized water three times, followed by immersing in DMF for 8 h. Afterward, the white powder was filtered from DMF and dried in an air oven for 12 h at 150°C. Finally, the fine powdered MIL-53 was further activated at 180°C under vacuum for 12 h.


## 2.3. Functionalization of MIL-53

MIL-53 particles (2.0 g) were dispersed in the mixed solvent of 2.6 g of deionized water, 60 mL of EtOH, and 1.36 g of aqueous ammonia. The suspension was stirred and sonicated in a round-bottomed flask at 60°C for 2 h. Then 1.44 g of APTMS was added dropwise into the mixture under stirring. The suspension reacted at room temperature for 12 h and then was centrifuged to obtain the modified product and washed with EtOH at least three times to remove residual APTMS. Finally, the aminosilane modified MIL-53 was dried under vacuum at 80°C for 24 h.


## 2.4. Mixed Matrix Hollow Fiber Membrane Preparation

### 2.4.1. Preparation of Spinning Dope

A certain amount of functionalized MIL-53 was added to a portion of the required NMP with stirred and sonicated alternatively for 45 min to obtain a well-dispersed suspension. Then MOFs filler was primed by addition of a dilute polymer solution into the suspension to ensure better adhesion. This mixture was stirred for 3 h and sonicated for 45 min until it displayed in uniform consistency. Then a required amount of EtOH was added with the remaining NMP into the suspension. Finally, the Ultem 1000 pellet was gradually added into the mixture to increase dope viscosity. After adding all the components, the suspension was mechanically stirred at 60°C for about 12 h to fully dissolve the polymer. For comparison purposes, the pure Ultem dope solution was prepared following an identical procedure. The polymer concentration in all dope solutions kept 33 wt% and the MOFs loading kept 15 wt% which was determined by(1)MOFsloadingwt%=wt.MOFswt.MOFs+wt.polymer×100%.


### 2.4.2. MMHFM Fabrication

Asymmetric hollow fiber membranes in this study were fabricated via the dry-wet spinning method. The homogeneous dope and bore fluid were coextruded from a spinneret after dope solution was degassed; then the nascent fiber entered a water coagulant bath with a range of spinning parameters (Table1) through the air gap distance and was wound up on a take-up drum. The spinning process was performed at 60°C and a filter was attached upstream of the spinneret to prevent impurity particles blocking the narrow spinneret orifice. Proper pressure was supplied by the nitrogen cylinder to maintain a constant spinning rate and a syringe pump was used to control the flow rate of bore fluid.Table 1
Detailed spinning parameters of hollow fiber membrane fabrication.
Spinning parameters Value Spinneret dimension (mm) o.d./i.d. = 0.70 : 0.35 Spinneret temperature (C°) 60 ± 2 Air gap distance (cm) 0.8–5.0 Bore fluid composition NMP : H2O = 10 wt% : 90 wt% NMP : H2O = 50 wt% : 50 wt% NMP : H2O = 90 wt% : 10 wt% Bore fluid flow rate (mL/min) 0.27 ± 0.02 External coagulant Tap water Temperature of external coagulant (C°) 18 ± 2The as-fabricated fibers were rinsed in flowing tap water for about 24 h to remove the remaining solvent. Then the fibers were exchanged by immersing in three successive aliquots of EtOH for 30 min, followed by 30 min immersion in three successive aliquots of n-hexane. Afterward, the hollow fiber membranes were dried at 70°C for 3 h.For sealing the microvoids or defects in the skin layer, each membrane module containing fibers was dip-coated by 3 wt% Sylgard 184 solution with a corresponding curing agent (10 wt% of Sylgard 184 PDMS) in petroleum ether. After coating for 30 min, the modules were placed into a 70°C oven and cured for 3 h after petroleum ether evaporation. The coated hollow fiber membranes were tested to evaluate gas permeation properties.


## 2.4.1. Preparation of Spinning Dope

A certain amount of functionalized MIL-53 was added to a portion of the required NMP with stirred and sonicated alternatively for 45 min to obtain a well-dispersed suspension. Then MOFs filler was primed by addition of a dilute polymer solution into the suspension to ensure better adhesion. This mixture was stirred for 3 h and sonicated for 45 min until it displayed in uniform consistency. Then a required amount of EtOH was added with the remaining NMP into the suspension. Finally, the Ultem 1000 pellet was gradually added into the mixture to increase dope viscosity. After adding all the components, the suspension was mechanically stirred at 60°C for about 12 h to fully dissolve the polymer. For comparison purposes, the pure Ultem dope solution was prepared following an identical procedure. The polymer concentration in all dope solutions kept 33 wt% and the MOFs loading kept 15 wt% which was determined by(1)MOFsloadingwt%=wt.MOFswt.MOFs+wt.polymer×100%.


## 2.4.2. MMHFM Fabrication

Asymmetric hollow fiber membranes in this study were fabricated via the dry-wet spinning method. The homogeneous dope and bore fluid were coextruded from a spinneret after dope solution was degassed; then the nascent fiber entered a water coagulant bath with a range of spinning parameters (Table1) through the air gap distance and was wound up on a take-up drum. The spinning process was performed at 60°C and a filter was attached upstream of the spinneret to prevent impurity particles blocking the narrow spinneret orifice. Proper pressure was supplied by the nitrogen cylinder to maintain a constant spinning rate and a syringe pump was used to control the flow rate of bore fluid.Table 1
Detailed spinning parameters of hollow fiber membrane fabrication.
Spinning parameters Value Spinneret dimension (mm) o.d./i.d. = 0.70 : 0.35 Spinneret temperature (C°) 60 ± 2 Air gap distance (cm) 0.8–5.0 Bore fluid composition NMP : H2O = 10 wt% : 90 wt% NMP : H2O = 50 wt% : 50 wt% NMP : H2O = 90 wt% : 10 wt% Bore fluid flow rate (mL/min) 0.27 ± 0.02 External coagulant Tap water Temperature of external coagulant (C°) 18 ± 2The as-fabricated fibers were rinsed in flowing tap water for about 24 h to remove the remaining solvent. Then the fibers were exchanged by immersing in three successive aliquots of EtOH for 30 min, followed by 30 min immersion in three successive aliquots of n-hexane. Afterward, the hollow fiber membranes were dried at 70°C for 3 h.For sealing the microvoids or defects in the skin layer, each membrane module containing fibers was dip-coated by 3 wt% Sylgard 184 solution with a corresponding curing agent (10 wt% of Sylgard 184 PDMS) in petroleum ether. After coating for 30 min, the modules were placed into a 70°C oven and cured for 3 h after petroleum ether evaporation. The coated hollow fiber membranes were tested to evaluate gas permeation properties.


## 2.5. Characterizations

The morphologies of functionalized MOFs and membranes were examined by scanning electron microscopy (SEM, Zeiss Supra 55 Sapphire). MOFs particles were tested without any dispersion. The membrane samples were frozen and broken off in liquid nitrogen and then sputtered with gold before SEM testing. MOFs and hollow fiber membranes were characterized by powder X-ray diffraction (XRD) using a PANalytical Empyrean diffractometer with Cu Kα radiation (λ = 0.15406 nm). The basal spacing was calculated by the Bragg’s equation:(2)nλ=2dsin⁡θ.Thermal stability of functionalized MIL-53, pure Ultem HFM, and MMHFM were measured by thermo-gravimetric analysis (TGA) at a heating rate of 10°C/min from room temperature to 800°C under nitrogen atmosphere using a TGA instrument (Netzsch STA449F3).


## 2.6. Pure Gas Permeation Measurement

Gas permeation experiments were conducted at 35°C with a testing pressure of 0.5 MPa. The permeation flow rate was measured with soap bubble flow meter and permeance (P/l) was calculated by the following:(3)Pl=ppVPRTVmAtΔp,where pp is the pressure of the permeate side (cmHg), VP is the volume of permeate gas during the test duration (cm3), Vm is the molar volume of ideal gas at standard condition [cm3 (STP)/mol], R is the universal gas constant, T is the absolute temperature (K),A is the permeation area (cm2), t is the test duration (s), and Δp is the trans-membrane pressure difference (cmHg). The permeance (P/l) values are commonly reported in the gas permeation unit GPU, 1 GPU = 1 × 10−6 cm3 (STP)/(cm2·s·cmHg). The ideal selectivity of gases i and j is defined as follows:(4)αi/j=P/liP/lj.For each sample, at least three membrane modules were prepared and tested as our previous work [3], and the average value of testing result (with standard deviation) was used to determine the gas separation performance.


## 3. Results and Discussion

### 3.1. Characterizations

Figure1 depicts SEM image of the functionalized MIL-53 by grafting aminosilane and MOFs particles appeared in the clump form due to the particle agglomeration. Therefore, the functionalized MOFs used as filler in MMHFM should be sufficiently dispersed before adding into spinning dope solution. The outer and inner surface, cross section, and skin layer of prepared pure Ultem HFM were shown in Figure 2. Morphology of MMHFM with 15 wt% filler loading was presented in Figure 3. The distribution of MOFs particles in Ultem matrix was homogeneous and there was no obvious aggregation as indicated by EDX mapping. Moreover, no surface cracks or interfacial voids revealed the excellent compatibility between the MOFs filler and polymer matrix. Additionally, more finger-like pores were generated in the outer region of MMHFM, which should be caused by instantaneous demixing with addition of MOFs particles.Figure 1
SEM image of functionalized MIL-53 powder.Figure 2
SEM images of cross section (a), outer surface (b), inner surface (c), and skin layer close-up (d, e) of pure Ultem HFM.
(a) (b) (c) (d) (e)Figure 3
SEM images of cross section (a), skin layer close-up (b), and outer surface (c); the inset is EDX mapping of outer surface (Al: red).
(a) (b) (c)The X-ray diffraction (XRD) patterns of functionalized MIL-53 and hollow fiber membranes are shown in Figure4. The Ultem/functionalized MIL-53 MMHFM exhibited new peaks compared with pure Ultem HFM, which indicated the presence of functionalized MIL-53 particles in the polymer matrix. The positions of extraneous peaks of MMHFM were not identical to the functionalized MOFs, suggesting the polymer chains intercalation into the clearance of functionalized MOFs particles. Additionally, the characteristic band of amorphous Ultem appeared around 16.1° that represented 5.5 Å of the d-space value. The band of MMHFM was slightly shifted to lower region which corresponded to a larger d-space. This shift revealed the changed arrangement of polymer chains packing with MOFs addition.Figure 4
X-ray diffractions of functionalized MIL-53, pure Ultem HFM, and Ultem/functionalized MIL-53 MMHFM.As shown in Figure5, the thermal gravimetric analysis of functionalized MIL-53, pure Ultem HFM, and MMHFM was performed to investigate the membrane thermal stability. A weight loss of functionalized MIL-53 before 140°C was caused by the adsorbed water evaporation. Another weight loss stage around 370–515°C was ascribed to decomposition of the grafted functional groups. At higher temperature, the organic linkers eliminated from the framework and functionalized MIL-53 transformed to Al2O3. With addition of functionalized MIL-53 particles, MMHFM achieved a higher decomposition temperature compared with pure Ultem HFM. The decomposition temperature increase for MOFs-containing MMHFM was attributed to higher energy required for polymer chains movement or segmentation via interaction between polymer matrix and functionalized MIL-53. Meanwhile, the shield effect of filler particles would also improve the thermal stability of MMHFM [32].Figure 5
TGA curves of functionalized MIL-53, pure Ultem HFM, and Ultem/functionalized MIL-53 MMHFM.


### 3.2. Effect of Solvent/Nonsolvent Ratio in Spinning Dope

The filler particles significantly affect the phase inversion as indicated by previous references [31, 33]. The addition of filler would cause the binodal line occurring at lower nonsolvent concentration which reduced the required nonsolvent for separation of dope solution. Figure 6 presents the effect of solvent/nonsolvent ratio in spinning dope on pure gas permeance and ideal selectivity of MMHFM containing the functionalized MIL-53. Gas permeance decreased with the decreased solvent/nonsolvent ratio which was ascribed to the formation of thicker skin layer as Ismail and Lai reported [34]. The evaporation of more volatile nonsolvent could increase polymer concentration of the nascent fiber outer part, resulting in the increment of skin layer thickness. The ideal CO2/N2 selectivity reached the highest value of 33.7 at the solvent/nonsolvent ratio of 9. However, excessive nonsolvent in dope caused early phase separation and composition path went across binodal line as indicated by Figure 7 which would trigger defects in the fiber skin in spite of the relatively large thickness of skin layer, thus reducing the ideal selectivity. This was consistent with our previous work [31]. At the solvent/nonsolvent ratio above 9, on the contrary, the polymer concentration in outermost region of nascent MMHFM was not high enough to form defect-free skin layer. Consequently, the ideal selectivity dropped obviously accompanying with increasing permeance.Figure 6
Gas permeance and ideal selectivity of MMHFM fabricated from spinning dope with different solvent/nonsolvent ratio.Figure 7
Phase diagram demonstrating phase inversion during dry-wet spinning process.


### 3.3. Effect of Spinning Condition

#### 3.3.1. Air Gap Distance

Besides the dope composition, the spinning condition was also critical to membrane performance. The outer part cross section of MMHFM prepared through different air gap distances was not identical, especially for the skin layer, as shown in Figure8. The MMHFM spun through 2 cm of air gap distance possessed fine asymmetric structure composed with thin dense skin layer and porous substructure. The functionalized MIL-53 incorporated MMHFM obtained 30.9 GPU of CO2 permeance and also exhibited excellent CO2/N2 selectivity of 34.7, as presented in Table 2. In contrast, the MMHFM prepared through a larger air gap distance (5 cm) had a thicker skin layer (Figure 8(a)), which could be explained by the delayed demixing during phase inversion [34]. The thicker selective layer increased gas transport resistance, which resulted in reduced gas permeance. Additionally, the ideal selectivity also decreased obviously, which should be ascribed to the absorption of moisture through the relatively large air gap. When the air gap distance decreased to 0.8 cm, it was difficult to observe the dense skin layer as shown in Figure 8(c). Correspondingly, the nonselective pinhole defects would occur in the skin layer inevitably. Therefore, CO2 permeance increased significantly to 39.8 GPU, but the ideal CO2/N2 selectivity was reduced to 24.8.Table 2
Effect of spinning condition on gas permeance and ideal selectivity of MMHFM.
Gap distance (cm) NMP content (wt%) Permeance (GPU) CO2/N2 selectivity CO2 N2 5 50 20.4 ± 1.0 0.69 ± 0.03 29.7 ± 0.7 2 50 30.9 ± 1.3 0.89 ± 0.03 34.7 ± 1.0 0.8 50 39.8 ± 1.4 1.61 ± 0.04 24.8 ± 1.0 2 10 28.3 ± 1.1 1.01 ± 0.04 28.0 ± 1.3 2 90 24.8 ± 1.4 0.74 ± 0.04 33.6 ± 1.5Figure 8
SEM images of outer part cross section of MMHFM prepared through different air gap distances ((a) 5 cm, (b) 2 cm, and (c) 0.8 cm).
(a) (b) (c)


#### 3.3.2. Bore Fluid Composition

The bore fluid composition was another important factor that influences the gas separation performance of MMHFM. Three different compositions of bore fluid were investigated in this work. The Ultem/functionalized MIL-53 MMHFM fabricated with the bore fluid containing 10 wt% NMP showed much lower CO2/N2 selectivity compared with that of MMHFM with 50 wt% NMP in the bore fluid. The high water content in the bore fluid would cause early phase separation through the air gap and quickly solidify the inner surface of MMHFM (Figure 9(a)), which would trigger the formation of defective skin layer. When the NMP content increased to 90 wt%, it could be observed that gas permeance decreased to 24.8 GPU for CO2 and 0.74 GPU for N2 (Table 2). The permeance decrease was ascribed to slow coagulation of polymer and formation of dense skin layer. Additionally, the hydrophobic functionalized MIL-53 particles tended to migrate to the inner surface presumably during the transfer between solvent and nonsolvent as indicated by Figure 9(c), which reduced the number of filler particles and fractional free volume in membrane. Therefore, the fast permeation channels decreased substantially, leading to relatively low gas permeance.Figure 9
SEM images of inner surface of MMHFMs with different bore fluid compositions ((a) 10% NMP, (b) 50% NMP, and (c) 90% NMP).
(a) (b) (c)


### 3.4. Comparison of Gas Separation Performance with Pure Ultem HFM

By varying the dope composition and spinning condition, the optimum permeation performance of MMHFM incorporated with functionalized MIL-53 was achieved. As shown in Table3, CO2 permeance increased significantly from 12.2 GPU for pure Ultem HFM to 30.9 GPU for MMHFM, which was attributed to the micropores of MOFs that offered extra permeation channels especially in the dense skin layer. The MOFs incorporation would disrupt polymer chain arrangement and thus expand interfacial space, also reducing the permeation resistance. Moreover, the ideal CO2/N2 selectivity was enhanced to 34.7 by a 37% increase at the same time. The alkyl chains grafted on MOFs endowed good particle dispersion in polymer matrix and improved polymer/filler interfacial affinity, which avoided the nonselective void formation. Additionally, the amino-functionalized MIL-53 with CO2 preferential adsorption also increased CO2 solubility [28, 35] and then facilitated the improvement of CO2/N2 selectivity.Table 3
Gas permeance and ideal selectivity of pure Ultem HFM and MMHFM.
Fiber Permeance (GPU) CO2/N2 selectivity C O 2 N 2 Pure Ultem HFM 12.2 ± 0.4 0.48 ± 0.02 25.4 ± 0.8 MMHFM 30.9 ± 1.3 0.89 ± 0.03 34.7 ± 1.0


### 3.5. Effect of Testing Temperature on Membrane Performance

The effect of testing temperature on gas permeation properties was also investigated in this work. As shown in Figure10, the trend of MMHFM was similar to that of pure Ultem HFM following the solution-diffusion based transport mechanism. When the measurement was conducted from 25°C to 55°C, the CO2 permeance of MMHFM increased about 56% and about 50% for pure Ultem HFM. The increase in testing temperature not only accelerated the gas diffusion rate but also promoted polymer chain mobility, which lowered the required activation energy for gas permeation and thus increased gas permeance [36]. However, the ideal selectivity decreased with increasing temperature. In order to further investigate the temperature dependency of gas permeance, an Arrhenius type equation was used to represent this activated process, as shown by (5)P=P0exp⁡-EpRT,whereP, P0,Ep,R, andT denote the gas permeation, preexponential factor, activation energy of permeation, universal gas constant, and the absolute temperature, respectively. The activation energy of permeation (Ep) is mainly affected by gas molecular size and solubility [37, 38]. The noninteracting gas with larger kinetic diameter like N2 has greater Ep than the gas with smaller kinetic diameter and better interaction with membrane like CO2 [38, 39], so N2 exhibits more temperature dependency of permeance. Hence, gas permeance increased but the selectivity decreased with temperature rising up. Additionally, MMHFM was not damaged by testing from lower temperature up to higher temperature and, returning to lower temperature several times, the gas separation performance was regained.Figure 10
Gas permeation properties of pure Ultem HFM and MMHFM plotted as a function of testing temperature.


## 3.1. Characterizations

Figure1 depicts SEM image of the functionalized MIL-53 by grafting aminosilane and MOFs particles appeared in the clump form due to the particle agglomeration. Therefore, the functionalized MOFs used as filler in MMHFM should be sufficiently dispersed before adding into spinning dope solution. The outer and inner surface, cross section, and skin layer of prepared pure Ultem HFM were shown in Figure 2. Morphology of MMHFM with 15 wt% filler loading was presented in Figure 3. The distribution of MOFs particles in Ultem matrix was homogeneous and there was no obvious aggregation as indicated by EDX mapping. Moreover, no surface cracks or interfacial voids revealed the excellent compatibility between the MOFs filler and polymer matrix. Additionally, more finger-like pores were generated in the outer region of MMHFM, which should be caused by instantaneous demixing with addition of MOFs particles.Figure 1
SEM image of functionalized MIL-53 powder.Figure 2
SEM images of cross section (a), outer surface (b), inner surface (c), and skin layer close-up (d, e) of pure Ultem HFM.
(a) (b) (c) (d) (e)Figure 3
SEM images of cross section (a), skin layer close-up (b), and outer surface (c); the inset is EDX mapping of outer surface (Al: red).
(a) (b) (c)The X-ray diffraction (XRD) patterns of functionalized MIL-53 and hollow fiber membranes are shown in Figure4. The Ultem/functionalized MIL-53 MMHFM exhibited new peaks compared with pure Ultem HFM, which indicated the presence of functionalized MIL-53 particles in the polymer matrix. The positions of extraneous peaks of MMHFM were not identical to the functionalized MOFs, suggesting the polymer chains intercalation into the clearance of functionalized MOFs particles. Additionally, the characteristic band of amorphous Ultem appeared around 16.1° that represented 5.5 Å of the d-space value. The band of MMHFM was slightly shifted to lower region which corresponded to a larger d-space. This shift revealed the changed arrangement of polymer chains packing with MOFs addition.Figure 4
X-ray diffractions of functionalized MIL-53, pure Ultem HFM, and Ultem/functionalized MIL-53 MMHFM.As shown in Figure5, the thermal gravimetric analysis of functionalized MIL-53, pure Ultem HFM, and MMHFM was performed to investigate the membrane thermal stability. A weight loss of functionalized MIL-53 before 140°C was caused by the adsorbed water evaporation. Another weight loss stage around 370–515°C was ascribed to decomposition of the grafted functional groups. At higher temperature, the organic linkers eliminated from the framework and functionalized MIL-53 transformed to Al2O3. With addition of functionalized MIL-53 particles, MMHFM achieved a higher decomposition temperature compared with pure Ultem HFM. The decomposition temperature increase for MOFs-containing MMHFM was attributed to higher energy required for polymer chains movement or segmentation via interaction between polymer matrix and functionalized MIL-53. Meanwhile, the shield effect of filler particles would also improve the thermal stability of MMHFM [32].Figure 5
TGA curves of functionalized MIL-53, pure Ultem HFM, and Ultem/functionalized MIL-53 MMHFM.


## 3.2. Effect of Solvent/Nonsolvent Ratio in Spinning Dope

The filler particles significantly affect the phase inversion as indicated by previous references [31, 33]. The addition of filler would cause the binodal line occurring at lower nonsolvent concentration which reduced the required nonsolvent for separation of dope solution. Figure 6 presents the effect of solvent/nonsolvent ratio in spinning dope on pure gas permeance and ideal selectivity of MMHFM containing the functionalized MIL-53. Gas permeance decreased with the decreased solvent/nonsolvent ratio which was ascribed to the formation of thicker skin layer as Ismail and Lai reported [34]. The evaporation of more volatile nonsolvent could increase polymer concentration of the nascent fiber outer part, resulting in the increment of skin layer thickness. The ideal CO2/N2 selectivity reached the highest value of 33.7 at the solvent/nonsolvent ratio of 9. However, excessive nonsolvent in dope caused early phase separation and composition path went across binodal line as indicated by Figure 7 which would trigger defects in the fiber skin in spite of the relatively large thickness of skin layer, thus reducing the ideal selectivity. This was consistent with our previous work [31]. At the solvent/nonsolvent ratio above 9, on the contrary, the polymer concentration in outermost region of nascent MMHFM was not high enough to form defect-free skin layer. Consequently, the ideal selectivity dropped obviously accompanying with increasing permeance.Figure 6
Gas permeance and ideal selectivity of MMHFM fabricated from spinning dope with different solvent/nonsolvent ratio.Figure 7
Phase diagram demonstrating phase inversion during dry-wet spinning process.


## 3.3. Effect of Spinning Condition

### 3.3.1. Air Gap Distance

Besides the dope composition, the spinning condition was also critical to membrane performance. The outer part cross section of MMHFM prepared through different air gap distances was not identical, especially for the skin layer, as shown in Figure8. The MMHFM spun through 2 cm of air gap distance possessed fine asymmetric structure composed with thin dense skin layer and porous substructure. The functionalized MIL-53 incorporated MMHFM obtained 30.9 GPU of CO2 permeance and also exhibited excellent CO2/N2 selectivity of 34.7, as presented in Table 2. In contrast, the MMHFM prepared through a larger air gap distance (5 cm) had a thicker skin layer (Figure 8(a)), which could be explained by the delayed demixing during phase inversion [34]. The thicker selective layer increased gas transport resistance, which resulted in reduced gas permeance. Additionally, the ideal selectivity also decreased obviously, which should be ascribed to the absorption of moisture through the relatively large air gap. When the air gap distance decreased to 0.8 cm, it was difficult to observe the dense skin layer as shown in Figure 8(c). Correspondingly, the nonselective pinhole defects would occur in the skin layer inevitably. Therefore, CO2 permeance increased significantly to 39.8 GPU, but the ideal CO2/N2 selectivity was reduced to 24.8.Table 2
Effect of spinning condition on gas permeance and ideal selectivity of MMHFM.
Gap distance (cm) NMP content (wt%) Permeance (GPU) CO2/N2 selectivity CO2 N2 5 50 20.4 ± 1.0 0.69 ± 0.03 29.7 ± 0.7 2 50 30.9 ± 1.3 0.89 ± 0.03 34.7 ± 1.0 0.8 50 39.8 ± 1.4 1.61 ± 0.04 24.8 ± 1.0 2 10 28.3 ± 1.1 1.01 ± 0.04 28.0 ± 1.3 2 90 24.8 ± 1.4 0.74 ± 0.04 33.6 ± 1.5Figure 8
SEM images of outer part cross section of MMHFM prepared through different air gap distances ((a) 5 cm, (b) 2 cm, and (c) 0.8 cm).
(a) (b) (c)


### 3.3.2. Bore Fluid Composition

The bore fluid composition was another important factor that influences the gas separation performance of MMHFM. Three different compositions of bore fluid were investigated in this work. The Ultem/functionalized MIL-53 MMHFM fabricated with the bore fluid containing 10 wt% NMP showed much lower CO2/N2 selectivity compared with that of MMHFM with 50 wt% NMP in the bore fluid. The high water content in the bore fluid would cause early phase separation through the air gap and quickly solidify the inner surface of MMHFM (Figure 9(a)), which would trigger the formation of defective skin layer. When the NMP content increased to 90 wt%, it could be observed that gas permeance decreased to 24.8 GPU for CO2 and 0.74 GPU for N2 (Table 2). The permeance decrease was ascribed to slow coagulation of polymer and formation of dense skin layer. Additionally, the hydrophobic functionalized MIL-53 particles tended to migrate to the inner surface presumably during the transfer between solvent and nonsolvent as indicated by Figure 9(c), which reduced the number of filler particles and fractional free volume in membrane. Therefore, the fast permeation channels decreased substantially, leading to relatively low gas permeance.Figure 9
SEM images of inner surface of MMHFMs with different bore fluid compositions ((a) 10% NMP, (b) 50% NMP, and (c) 90% NMP).
(a) (b) (c)


## 3.3.1. Air Gap Distance

Besides the dope composition, the spinning condition was also critical to membrane performance. The outer part cross section of MMHFM prepared through different air gap distances was not identical, especially for the skin layer, as shown in Figure8. The MMHFM spun through 2 cm of air gap distance possessed fine asymmetric structure composed with thin dense skin layer and porous substructure. The functionalized MIL-53 incorporated MMHFM obtained 30.9 GPU of CO2 permeance and also exhibited excellent CO2/N2 selectivity of 34.7, as presented in Table 2. In contrast, the MMHFM prepared through a larger air gap distance (5 cm) had a thicker skin layer (Figure 8(a)), which could be explained by the delayed demixing during phase inversion [34]. The thicker selective layer increased gas transport resistance, which resulted in reduced gas permeance. Additionally, the ideal selectivity also decreased obviously, which should be ascribed to the absorption of moisture through the relatively large air gap. When the air gap distance decreased to 0.8 cm, it was difficult to observe the dense skin layer as shown in Figure 8(c). Correspondingly, the nonselective pinhole defects would occur in the skin layer inevitably. Therefore, CO2 permeance increased significantly to 39.8 GPU, but the ideal CO2/N2 selectivity was reduced to 24.8.Table 2
Effect of spinning condition on gas permeance and ideal selectivity of MMHFM.
Gap distance (cm) NMP content (wt%) Permeance (GPU) CO2/N2 selectivity CO2 N2 5 50 20.4 ± 1.0 0.69 ± 0.03 29.7 ± 0.7 2 50 30.9 ± 1.3 0.89 ± 0.03 34.7 ± 1.0 0.8 50 39.8 ± 1.4 1.61 ± 0.04 24.8 ± 1.0 2 10 28.3 ± 1.1 1.01 ± 0.04 28.0 ± 1.3 2 90 24.8 ± 1.4 0.74 ± 0.04 33.6 ± 1.5Figure 8
SEM images of outer part cross section of MMHFM prepared through different air gap distances ((a) 5 cm, (b) 2 cm, and (c) 0.8 cm).
(a) (b) (c)


## 3.3.2. Bore Fluid Composition

The bore fluid composition was another important factor that influences the gas separation performance of MMHFM. Three different compositions of bore fluid were investigated in this work. The Ultem/functionalized MIL-53 MMHFM fabricated with the bore fluid containing 10 wt% NMP showed much lower CO2/N2 selectivity compared with that of MMHFM with 50 wt% NMP in the bore fluid. The high water content in the bore fluid would cause early phase separation through the air gap and quickly solidify the inner surface of MMHFM (Figure 9(a)), which would trigger the formation of defective skin layer. When the NMP content increased to 90 wt%, it could be observed that gas permeance decreased to 24.8 GPU for CO2 and 0.74 GPU for N2 (Table 2). The permeance decrease was ascribed to slow coagulation of polymer and formation of dense skin layer. Additionally, the hydrophobic functionalized MIL-53 particles tended to migrate to the inner surface presumably during the transfer between solvent and nonsolvent as indicated by Figure 9(c), which reduced the number of filler particles and fractional free volume in membrane. Therefore, the fast permeation channels decreased substantially, leading to relatively low gas permeance.Figure 9
SEM images of inner surface of MMHFMs with different bore fluid compositions ((a) 10% NMP, (b) 50% NMP, and (c) 90% NMP).
(a) (b) (c)


## 3.4. Comparison of Gas Separation Performance with Pure Ultem HFM

By varying the dope composition and spinning condition, the optimum permeation performance of MMHFM incorporated with functionalized MIL-53 was achieved. As shown in Table3, CO2 permeance increased significantly from 12.2 GPU for pure Ultem HFM to 30.9 GPU for MMHFM, which was attributed to the micropores of MOFs that offered extra permeation channels especially in the dense skin layer. The MOFs incorporation would disrupt polymer chain arrangement and thus expand interfacial space, also reducing the permeation resistance. Moreover, the ideal CO2/N2 selectivity was enhanced to 34.7 by a 37% increase at the same time. The alkyl chains grafted on MOFs endowed good particle dispersion in polymer matrix and improved polymer/filler interfacial affinity, which avoided the nonselective void formation. Additionally, the amino-functionalized MIL-53 with CO2 preferential adsorption also increased CO2 solubility [28, 35] and then facilitated the improvement of CO2/N2 selectivity.Table 3
Gas permeance and ideal selectivity of pure Ultem HFM and MMHFM.
Fiber Permeance (GPU) CO2/N2 selectivity C O 2 N 2 Pure Ultem HFM 12.2 ± 0.4 0.48 ± 0.02 25.4 ± 0.8 MMHFM 30.9 ± 1.3 0.89 ± 0.03 34.7 ± 1.0


## 3.5. Effect of Testing Temperature on Membrane Performance

The effect of testing temperature on gas permeation properties was also investigated in this work. As shown in Figure10, the trend of MMHFM was similar to that of pure Ultem HFM following the solution-diffusion based transport mechanism. When the measurement was conducted from 25°C to 55°C, the CO2 permeance of MMHFM increased about 56% and about 50% for pure Ultem HFM. The increase in testing temperature not only accelerated the gas diffusion rate but also promoted polymer chain mobility, which lowered the required activation energy for gas permeation and thus increased gas permeance [36]. However, the ideal selectivity decreased with increasing temperature. In order to further investigate the temperature dependency of gas permeance, an Arrhenius type equation was used to represent this activated process, as shown by (5)P=P0exp⁡-EpRT,whereP, P0,Ep,R, andT denote the gas permeation, preexponential factor, activation energy of permeation, universal gas constant, and the absolute temperature, respectively. The activation energy of permeation (Ep) is mainly affected by gas molecular size and solubility [37, 38]. The noninteracting gas with larger kinetic diameter like N2 has greater Ep than the gas with smaller kinetic diameter and better interaction with membrane like CO2 [38, 39], so N2 exhibits more temperature dependency of permeance. Hence, gas permeance increased but the selectivity decreased with temperature rising up. Additionally, MMHFM was not damaged by testing from lower temperature up to higher temperature and, returning to lower temperature several times, the gas separation performance was regained.Figure 10
Gas permeation properties of pure Ultem HFM and MMHFM plotted as a function of testing temperature.


## 4. Conclusion

MMHFM containing 15 wt% functionalized MIL-53 was fabricated via the dry-wet phase inversion method. The functionalized MIL-53 particles dispersed homogeneously in the polymer matrix and good interfacial affinity was achieved without nonselective voids or cracks. MMHFM with incorporation of MOFs obtained a higher decomposition temperature compared with pure Ultem HFM because of the difficulty for polymer chain movement and the shield effect of filler particles. MMHFM spun from the dope with appropriate solvent ratio (solvent/nonsolvent ratio was equal to 9) achieved excellent separation performance. Moreover, the spinning condition was also optimized and was better to be chosen 2 cm of air gap distance and 50% NMP content in bore fluid composition. By optimizing dope composition, air gap distance, and bore fluid composition, CO2 permeance and ideal CO2/N2 selectivity of MMHFM reached 30.9 GPU and 34.7, respectively. With respect to the testing temperature, the permeation trend of MMHFM was similar to that of pure Ultem HFM following the solution-diffusion mechanism.



---

*Source: 2548957-2017-02-26.xml*