Quaternized Diaminobutane/Poly(vinyl alcohol) Cross-Linked Membranes for Acid Recovery via Diffusion Dialysis

Diffusion dialysis (DD) using anion exchange membranes (AEM) is an effective process for acid recovery and requires the preparation of suitable materials for AEMs, characterized by unique ions transport properties. In this work, novel AEMs composed of quaternized diaminobutane (QDAB) and poly(vinyl alcohol) (PVA) were cross-linked by tetraethoxysilane (TEOS) via the sol–gel process. The prepared AEMs were systematically characterized by Fourier-transform infrared (FTIR) spectroscopy, ion-exchange capacity (IEC) analysis, thermo gravimetric analysis (TGA), water uptake, linear expansion ratio (LER), and mechanical strength determination, scanning electron microscopy (SEM), and DD performance analysis for acid recovery using a hydrochloric acid/iron chloride (HCl/FeCl2) aqueous mixture and varying the QDAB content. The prepared AEMs exhibited IEC values between 0.86 and 1.46 mmol/g, water uptake values within 71.3 and 47.8%, moderate thermal stability, tensile strength values in the range of 26.1 to 41.7 MPa, and elongation from 68.2 to 204.6%. The dialysis coefficient values were between 0.0186 and 0.0295 m/h, whereas the separation factors range was 24.7–44.1 at 25 °C. The prepared membranes have great potential for acid recovery via diffusion dialysis.


Introduction
Wastewater is produced in various contexts including hydrometallurgy, metal refining, steel processing, aluminum etching, electroplating, and resin regeneration. It contains inorganic acids and metal ions [1,2]. The direct disposal of these acid effluents in the environment without treatment not only wastes useful acids but also is a great threat to human health and the environment [3][4][5]. The traditional methods that have been applied to treat acidic waste comprise extraction [6], ion exchange [7], electrodialysis [8], alkali neutralization [9], and pyrohydrolysis [10]. In comparison with all separationbased methods, anion exchange membrane (AEM)-based diffusion dialysis (DD) is highly preferable to treat acid wastes due to its energy efficiency, as electric power is only required for pumping the liquid streams into the dialyzer system and it is of easy installation, that

Synthesis of Quaternized Diaminobutane (QDAB)
QDAB was prepared by the reaction of 1,4-diaminobutane and GTMAC in DMSO, as shown in reaction Scheme 1. Firstly, 1 g of 1,4-diaminobutane (0.01134 mol) and 12 mL of DMSO as solvent were mixed in a 50 mL round-bottom flask with continuous magnetic stirring at 85 • C for 30 min. In this transparent reaction mixture, a calculated amount of GTMAC (3.44 g, 0.02269 mol) was added. Stirring was continued at 85 • C for 12 h to complete the reaction. A viscous and homogeneous solution of QDAB was obtained, cooled down to room temperature, and kept in a sealed bottle for further use. mixed with PVA along with the TEOS cross-linker, then AEMs were fabricated. The innovation of this work is the dispersion of QDAB in PVA cross-linked membranes, which, according to the best of our knowledge, has never been reported for acid recovery via DD. QDAB possesses two ionic sites serving as fast charge carriers and can enhance the ionic diffusivity during DD. The cross-linking agent TEOS ensured the thermal and mechanical stability of the membrane by changing its morphological properties and hydrophilicity [40]. Moreover, Fourier-transform infrared spectroscopy (FTIR), IEC, water uptake, and swelling degree determination, thermo gravimetric analysis (TGA), scanning electron microscopy (SEM), and mechanical strength analysis of the prepared membranes were carried out. The membranes were finally tested for acid recovery and separation performance by conducting diffusion dialysis experiments using an HCl/FeCl2 aqueous mixture.

Synthesis of Quaternized Diaminobutane (QDAB)
QDAB was prepared by the reaction of 1,4-diaminobutane and GTMAC in DMSO, as shown in reaction Scheme 1. Firstly, 1 g of 1,4-diaminobutane (0.01134 mol) and 12 mL of DMSO as solvent were mixed in a 50 mL round-bottom flask with continuous magnetic stirring at 85 °C for 30 min. In this transparent reaction mixture, a calculated amount of GTMAC (3.44 g, 0.02269 mol) was added. Stirring was continued at 85 °C for 12 h to complete the reaction. A viscous and homogeneous solution of QDAB was obtained, cooled down to room temperature, and kept in a sealed bottle for further use. Scheme 1. Reaction scheme for the preparation of quaternized diaminobutane. Scheme 1. Reaction scheme for the preparation of quaternized diaminobutane.

Preparation of QDAB/PVA Membranes
The QDAB/PVA AEMs were prepared using the standard sol-gel process, as shown in the proposed reaction Scheme 2. First, 1 g of PVA was dissolved in 19  solution was added to the prepared PVA solution. Then, 0.2 g of TEOS (20 wt. % to PVA) cross-linker along with a small quantity of 0.1 M HCl solution (as a catalyst) was carefully added in the reaction mixture. The reaction mixture was stirred at 60 • C for 24 h on a hot plate to complete the sol-gel reaction by the hydrolysis of silane. The resulting gel mixture was cast on a Petri dish and dried in a preheated oven at 60 • C for 24 h. The obtained membrane was carefully peeled off the Petri dish with the help of a knife blade. Finally for thermal cross-linking by heat treatment, the AEMs were heated from 70 • C to 130 • C at the heating rate of 10 • C/h and kept at 130 • C for 4 h to ensure a complete conversion into hybrid membranes. The thickness of the membrane was maintained around 165 to 190 µm. Five different membranes, mentioned in Table 1, were prepared by varying the amount of QDAB from 30 wt. % to 70 wt. % of PVA and were coded as QDAB-30, QDAB-40, QDAB-50, QDAB-60, and QDAB-70, respectively.

Preparation of QDAB/PVA Membranes
The QDAB/PVA AEMs were prepared using the standard sol-gel process, as shown in the proposed reaction Scheme 2. First, 1 g of PVA was dissolved in 19 g DMSO with continuous stirring for 4 h at 85 °C. A clear homogeneous solution of PVA (5 wt. %) was obtained and cooled down to 60 °C. A suitable amount of QDAB with respect to PVA in DMSO solution were separately stirred for 30 min at ambient conditions, and the QDAB solution was added to the prepared PVA solution. Then, 0.2 g of TEOS (20 wt. % to PVA) cross-linker along with a small quantity of 0.1 M HCl solution (as a catalyst) was carefully added in the reaction mixture. The reaction mixture was stirred at 60 °C for 24 h on a hot plate to complete the sol-gel reaction by the hydrolysis of silane. The resulting gel mixture was cast on a Petri dish and dried in a preheated oven at 60 °C for 24 h. The obtained membrane was carefully peeled off the Petri dish with the help of a knife blade. Finally for thermal cross-linking by heat treatment, the AEMs were heated from 70 °C to 130 °C at the heating rate of 10 °C/h and kept at 130 °C for 4 h to ensure a complete conversion into hybrid membranes. The thickness of the membrane was maintained around 165 to 190 μm. Five different membranes, mentioned in Table 1, were prepared by varying the amount of QDAB from 30 wt. % to 70 wt. % of PVA and were coded as QDAB-30, QDAB-40, QDAB-50, QDAB-60, and QDAB-70, respectively. Scheme 2. Preparation procedure of the QDAB-cross-linked PVA membrane through the sol-gel process with TEOS.

Fourier-Transform Infrared (FTIR) Spectroscopy
FTIR spectroscopic analysis of the PVA hybrid membrane was evaluated with an IR Shimadzu, Prestige-21 (Japan) spectrometer attenuated with a Horizontal Attenuated Total Reflectance (HATR) equipment. The spectral range of the experiment was 4000-400 cm −1 , and 100 scans were collected per spectrum at a resolution of 4 cm −1 . The experiment was performed with air as its background.  Reflectance (HATR) equipment. The spectral range of the experiment was 4000-400 cm −1 , and 100 scans were collected per spectrum at a resolution of 4 cm −1 . The experiment was performed with air as its background.

Ion-Exchange Capacity (IEC)
The IEC of the prepared membranes was determined to investigate the content of interchangeable ionic groups in the membranes using the Mohr method. A dried membrane sample was weighed and soaked in a 1.0 M NaCl solution for 24 h at room temperature to convert the ion-exchange groups into Cl − . After this, the sample was washed with deionized water to remove excessive NaCl and immersed in 50 mL of a 0.05 mol/L Na 2 SO 4 aqueous solution for 48 h to replace the Cl − ions by SO 4 2− ions. The concentration of the released Cl − ions in solution was determined by titration using a 0.05 mol/L AgNO 3 solution, and K 2 CrO 4 was used as an indicator [41]. The IEC (mmol/g) of the membrane was determined with Equation (1): where, C AgNO 3 , V AgNO 3 , and W dry represent the molar concentration (mol/L) of the AgNO 3 solution, the volume (mL) of the AgNO 3 solution consumed, and the dry weight (g) of the membrane, respectively.

Water Uptake and Linear Expansion Ratio
Water uptake was measured to investigate the hydrophilicity of the membrane. Small pieces of the membranes were dried in a vacuum oven at 65 • C for 24 h. The dried pieces of the membranes were weighed and then soaked in deionized water at room temperature for 24 h. The wet membrane pieces were weighed after wiping out the extra water from the membrane surface with a blotting paper. The water uptake (%) was determined [42] using Equation (2): where W wet and W dry represent the weight of wet and dry membranes, respectively. The linear expansion ratio (LER) was calculated to determine membrane stability. The dry membrane samples (3 cm × 1 cm) were immersed in deionized water for 24 h. LER (%) was measured using the following Equation (3) [43]: where L dry and L wet represent the length of dry and wet membranes, respectively.

Thermal Stability
The thermal properties were characterized by thermo gravimetric analysis (TGA) using a TGA Mettler Toledo analyzer at 10 • C/min heating rate; the temperature program used for TGA involved a temperature increase from room temperature to 800 • C. Nitrogen gas with a flow rate of 15 mL/min was used to obtain an inert atmosphere.

Mechanical Properties
Mechanical stability of QDAB hybrid membranes was determined with the help of the U-CAN Dynatex tensile tester (UT-2080, Taiwan) having crosshead speed of 100 mm/min. The dumbbell-shaped sample had a length of 25 mm between the jaws and a width of 5 mm. The experiment was performed at a relative humidity of 25 ± 2% and at a temperature of 25 • C.

Scanning Electron Microscopy
The morphology of the prepared membranes was examines through SEM using Jeol (JSM-6490A). The surface images of the membranes were collected under low vacuum, at a voltage of 5 KV.

Acid Recovery Experiment
The DD experiment was performed using a cell with two compartments, which were divided by the membrane, with an effective area of about 6.2 cm 2 . The membranes were dipped in the feed solution for 2 h before the test. One compartment of the dialysis cell was filled with 100 mL of feed solution consisting of a HCl/FeCl 2 aqueous mixture (1 M HCl/0.25 M FeCl 2 ), and the other compartment was filled with 100 mL of deionized water as the dialysate. Both compartments of the dialysis cell were stirred continuously with the help of magnetic stirrer at an equal speed to avoid concentration polarization. The experiment was performed at 25 • C for 1 h, and then from both compartments of the cell, feed and permeate solutions were removed. The concentration of H + and Fe 2+ ions in feed and permeate were measured by titration using standard solutions of Na 2 CO 3 , with methyl orange and KMnO 4 as indicators, respectively.
The dialysis coefficient (U) was calculated using the following Equation (4) [38]: where M indicates the amount of component transported in moles, A is the effective area of the membrane (m 2 ), t stands for time in h, and ∆C is the logarithm average concentration (mol/m 3 ) between the two compartments, which is given by Equation (5) [36,38]: where C 0 f and C t f are the concentrations of the feed solution at time 0 and t, respectively, whereas the concentration of the dialysate at t time is C t d . The separation factor (S) was determined by the ratio of (two dialysis coefficients) the acid dialysis coefficient (U H ) and the dialysis coefficient of ferrous ion (U Fe ) in the solution. The S value was determined using Equation (6):

FTIR Spectra Analysis
The FTIR spectra of pristine PVA, QDAB, TEOS, and cross-linked QDAB/PVA AEMs are shown in Figure 1. In the spectra of QDAB, the peaks at 1925 and 1645 cm −1 correspond to the stretching of -CH 2 and -CH, and the peak at 1469 cm −1 is due to the stretching of C−N from the ammonium groups. These peaks are also observed in the spectra of the prepared membranes. The band in the 3100-3550 cm −1 region in QDAB and PVA corresponds to the stretching vibration of −OH groups [38]. In cross-linked QDAB/PVA AEMs, the absorption band in the region 1255-1350 cm −1 represents the secondary C−N stretching vibration of QDAB [44]. The strong and broad band in the 3100-3550 cm −1 region is assigned to the stretching vibration of −OH groups [39]. The band of the −CH stretching vibration of alkyl groups is observed around 2925 cm −1 [45]. The characteristics band of the quaternary ammonium [-N + (CH 3 ) 3 ] group is observed at 1469 cm −1 [13,38]. The stretching bands of Si−O−C and Si−O−Si linkages are observed in the region from 1052 to 1150 cm −1 [46,47], while a small peak at 945 cm −1 is attributed to the stretching vibration of the silanol (Si−OH) group [48]. The intensity of the stretching vibration of the -OH band increased with the increase in the QDAB content, as shown in Figure 1.

Ion-Exchange Capacity
The IEC value was measured using Mohr's titration method to confirm the charged nature of the AEMs. The influence of QDAB content on the IEC value is depicted in Figure  2 and reported in Table 1. The IEC represents the charged nature of the membrane and is directly proportional to functional groups fixed in the membrane matrix. The IEC was mainly contributed by the −N + (CH3)3Cl − functional groups present inside the membrane matrix. The IEC values of the QDAB membranes increased from 0.86 to 1.46 mmol/g with the increase in the content of QDAB. These IEC values are comparable to or higher than those reported for different AEMs [23,32,49,50].

Ion-Exchange Capacity
The IEC value was measured using Mohr's titration method to confirm the charged nature of the AEMs. The influence of QDAB content on the IEC value is depicted in Figure 2 and reported in Table 1. The IEC represents the charged nature of the membrane and is directly proportional to functional groups fixed in the membrane matrix. The IEC was mainly contributed by the −N + (CH 3 ) 3 Cl − functional groups present inside the membrane matrix. The IEC values of the QDAB membranes increased from 0.86 to 1.46 mmol/g with the increase in the content of QDAB. These IEC values are comparable to or higher than those reported for different AEMs [23,32,49,50].
The IEC values of QDAB AEMs increased with the increase in the amount of QDAB, resulting in greater charge density. These results indicated the successful cross-linking of QDAB with the PVA chain; the uncross-linked QDAB was washed out during the membrane fabrication process and showed a constant IEC value.

Water Uptake and Linear Expansion Ratio
The water uptake and linear expansion ratio of the prepared AEMs are presented in Table 1 and Figure 3. The water uptake values of QDAB AEMs were in the range of 71.3-147.8%. Moreover, the results showed that the water uptake values increased by increasing the content of quaternary ammonium groups in hybrid PVA blend membranes. The water uptake of QDAB membranes showed an increasing trend similar to that of the IEC values, and QDAB-70 exhibited the highest water uptake values. The higher hydrophilic nature of the AEMs assisted the transport of ions [13], and more ions were transported inside membrane matrices with high water uptake.  The IEC values of QDAB AEMs increased with the increase in the amount of QDAB, resulting in greater charge density. These results indicated the successful cross-linking of QDAB with the PVA chain; the uncross-linked QDAB was washed out during the membrane fabrication process and showed a constant IEC value.

Water Uptake and Linear Expansion Ratio
The water uptake and linear expansion ratio of the prepared AEMs are presented in Table 1 and Figure 3. The water uptake values of QDAB AEMs were in the range of 71.3-147.8%. Moreover, the results showed that the water uptake values increased by increasing the content of quaternary ammonium groups in hybrid PVA blend membranes. The water uptake of QDAB membranes showed an increasing trend similar to that of the IEC values, and QDAB-70 exhibited the highest water uptake values. The higher hydrophilic nature of the AEMs assisted the transport of ions [13], and more ions were transported inside membrane matrices with high water uptake.
The linear expansion ratio (LER) is used to estimate the dimensional stability of AEMs during the DD process. As shown in Figure 3, as the QDAB loading (30 wt. % to 70 wt. %) increased in the PVA matrix, LER increased from 28.7 to 39.5%. These results indicate the flexibility of the AEMs, which means that the membranes are not brittle and  [15]. Hence, these bonds supplied strength to resist linear expansion. It was found that the membrane with the highest water uptake showed the higher LER. TEOS was used as a cross-linker, and the amount of TEOS was the same for all prepared membranes; the QDAB content increased, which produced a decrease in the degree of cross-linking in the membrane. Therefore, the cross-linking degree decreased in membranes with a higher QDAB amount and led to an increase in LER.

Thermal Stability of QDAB AEMs
The thermal stability of the QDAB members was evaluated using TGA, and the results are presented in Figure 4. Each thermogram shoes mainly four weight loss steps. The first step was associated with the removal of bound and unbound water from the membrane matrix, dequaternization occurred in the second step, the next step involved the removal of hydroxyl groups from PVA, and finally the degradation of the membrane matrix was completed. The first step of weight loss in the temperature range of 25-200 °C is attributed to dehydration, i.e., the removal of bounded or unbounded water molecules and water produced from the condensation reaction during the sol-gel process from the membrane matrix [28]. With the increase in the amount of QDAB in the PVA matrix, the hydrophilicity of the membrane increased; therefore, in this step, the QDAB-70 membrane showed the largest weight loss in comparison with the other QDAB membranes. The The linear expansion ratio (LER) is used to estimate the dimensional stability of AEMs during the DD process. As shown in Figure 3, as the QDAB loading (30 wt. % to 70 wt. %) increased in the PVA matrix, LER increased from 28.7 to 39.5%. These results indicate the flexibility of the AEMs, which means that the membranes are not brittle and showed swelling resistance. TEOS reacted with −OH group of PVA via the sol-gel reaction, with the formation of Si−O−Si and Si−O−C linkages which can significantly improve membrane stability [15]. Hence, these bonds supplied strength to resist linear expansion. It was found that the membrane with the highest water uptake showed the higher LER. TEOS was used as a cross-linker, and the amount of TEOS was the same for all prepared membranes; the QDAB content increased, which produced a decrease in the degree of cross-linking in the membrane. Therefore, the cross-linking degree decreased in membranes with a higher QDAB amount and led to an increase in LER.

Thermal Stability of QDAB AEMs
The thermal stability of the QDAB members was evaluated using TGA, and the results are presented in Figure 4. Each thermogram shoes mainly four weight loss steps. The first step was associated with the removal of bound and unbound water from the membrane matrix, dequaternization occurred in the second step, the next step involved the removal of hydroxyl groups from PVA, and finally the degradation of the membrane matrix was completed. The first step of weight loss in the temperature range of 25-200 • C is attributed to dehydration, i.e., the removal of bounded or unbounded water molecules and water produced from the condensation reaction during the sol-gel process from the membrane matrix [28]. With the increase in the amount of QDAB in the PVA matrix, the hydrophilicity of the membrane increased; therefore, in this step, the QDAB-70 membrane showed the largest weight loss in comparison with the other QDAB membranes. The weight loss in the second step from 200 to 330 • C is associated with the decomposition of quaternary ammonium groups and the rupture of the PVA chain. Here, QDAB-70 exhibited a higher weight loss as compared to the other prepared AEMs. This was due to the increase in the amount of −N + (CH 3 ) 3 functional groups which started to degrade at a relatively low temperature [51]. The next step from 330 to 490 • C is attributed to the elimination of hydroxyl groups from PVA [52]. In this step, increasing the content of QDAB in the membrane matrix improved the thermal stability of AEMs. The final degradation stage from 490 • C onwards is the carbonization of the main backbone of polymer chains to ash residue [53]. The incorporation of QDAB functionality in PVA enhanced the membranes' thermal stability in this step.  The TGA thermograms also demonstrated that QDAB has a vital role in thermal stability, and the prepared QDAB AEMs are thermally stable in nature. Initially, the QDAB-70 membrane demonstrated higher weight loss compared to the other membranes. as shown in Table 2. Afterward, the QDAB-70 membrane became thermally stable and The TGA thermograms also demonstrated that QDAB has a vital role in thermal stability, and the prepared QDAB AEMs are thermally stable in nature. Initially, the QDAB-70 membrane demonstrated higher weight loss compared to the other membranes. as shown in Table 2. Afterward, the QDAB-70 membrane became thermally stable and showed less weight loss compared to QDAB-60 in the degradation stage. Similarly, QDAB-50 and QDAB-40 AEMs underwent a more limited weight loss compared to the QDAB-30 membrane. For example, a 40% weight loss was observed at 381, 376, 371, 365, and 358 • C for the QDAB-70, QDAB-60, QDAB-50, QDAB-40, and QDAB-30 membranes, respectively. Similarly, 60% weight loss was observed at 441, 438, 421, 411, and 396 • C for the QDAB-70, QDAB-60, QDAB-50, QDAB-40, and QDAB-30 membranes, respectively.

Mechanical Strength of QDAB Membranes
The influence of QDAB content on the mechanical properties of the membranes is shown in Figure 5. The TS values of the prepared AEMs were in the range of 26.1-41.7 MPa, whereas the Eb values varied from 68.2% to 204.6%. These values are much higher than those of hybrid PVA/SiO 2 anion exchange membranes with multi-silicon copolymer (TS: 7-12 MPa, Eb: 42-97%) [49], which indicates the superior mechanical strength of our QDAB hybrid membranes compared to other membrane described in the literature. It has been found that an increase in the content of QDAB resulted in a decrease of TS and an improvement of Eb values. The QDAB-70 membrane had high flexibility and showed a maximum Eb value as well as a low TS value. The enhancement of the Eb values with the maximum dosage of QDAB is attributed to soft hydrophilic sites in the QDAB compound, which acts as a diluent that reduces the interaction between the long chains of PVA. Thus, it reduces the tensile strength and enhances the mobility of the PVA chains, leading to the maximum Eb value of the QDAB-70 membrane [54]. Similar results have been reported for hybrid membranes and attributed to the miscibility and cross-linking of It has been found that an increase in the content of QDAB resulted in a decrease of TS and an improvement of Eb values. The QDAB-70 membrane had high flexibility and showed a maximum Eb value as well as a low TS value. The enhancement of the Eb values with the maximum dosage of QDAB is attributed to soft hydrophilic sites in the QDAB compound, which acts as a diluent that reduces the interaction between the long chains of PVA. Thus, it reduces the tensile strength and enhances the mobility of the PVA chains, leading to the maximum Eb value of the QDAB-70 membrane [54]. Similar results have been reported for hybrid membranes and attributed to the miscibility and cross-linking of organic and inorganic moieties inside a hybrid polymeric membrane [55].

Morphological Analysis
The influence of QDAB content on membrane morphology was studied by SEM and arise presented in Figure 6. SEM images suggested that the membrane surface was compact and dense, without any holes or cracks. Figure 6e shows some aggregates on the surface of the QDAB-70 membrane due to the accelerated hydrolysis of TEOS with the increase in QDAB content. It was observed that QDAB was uniformly distributed promoting a homogeneous structure without any evidence of phase separation. The homogeneity of the AEMs indicated the compatibility between the QDAB anion exchange precursor and the PVA matrix. The QDAB anion precursor is effectively cross-linked between PVA and TEOS with covalent and hydrogen bonds through the sol-gel reaction [34,36]. The aggregations of particles increased in the AEMs with the increase in the amount of QDAB, as compared other QDAB AEMs. In the QDAB-70 membrane, a slight phase separation was observed because of the high anionic content [32]. Therefore, a larger aggregation of silica-rich particles may occur in the QDAB-70 membrane.

Acid Recovery Performance of QDAB AEMs via Diffusion Dialysis (DD)
Acidic waste solutions mostly contain metal ions and inorganic acid, which is usually generated during different industrial processes such as metal electrolysis and metallurgical and acid cleaning processes [10]. Therefore, to analyze the DD performance properties for acid recovery, QDAB AEMs were employed to separate a HCl/FeCl 2 aqueous solution (1 M HCl/0.25 M FeCl 2 ) used as a model aqueous waste feed to assess their potential for application in acid recovery. The DD results of AEMs with different wt. % of QDAB in the PVA matrix in terms of acid dialysis coefficients (U H ), separation factor (S,) and dialysis coefficient ferrous ion (U Fe ) at 25 • C are shown in Figure 7.
As shown in Figure 7, the acid dialysis coefficients (U H ) values of QDAB AEMs increased rapidly by increasing the content of QDAB, which was attributed to −N + (CH 3 ) 3 functional groups that enhanced the interaction between the membrane matrix and ions. The obtained U H values were in the range of 0.0186-0.0295 m/h and were relatively higher than those of PVA/QUDAP AEMs (0.008-0.0222 m/h at 25 • C) [27]. It was found that the QDAB-70 membrane with 70 wt. % of QDAB content exhibited the highest U H value of 0.0295 m/h. The U H value of QDAB-70 AEM was higher than the U H values of a multi-silicon/BPPO-based membrane (0.025 m/h) [22], a PVA-based hybrid AEM (0.018 m/h) [38], and a commercial DF-120 membrane (0.009 m/h) [34].
The mechanism of ion transport from the membrane matrix can be depicted by considering the action of diffusion dialysis, the hydrophilicity, hydrogen bonding, ion exchange of functional groups, and structure of the membrane matrix [36,49]. The Si−OH group from TEOS and −OH groups of PVA transport the H + ions from the membrane matrix through hydrogen bonds. The existence of hydrogen bonds is beneficial and accelerate the migration of H + ions through the membrane [36]. QDAB hybrid membranes possess −N + (CH 3 ) 3 functional groups that act as ion exchange sites to facilitate the migration of Cl − ions. Therefore, an increase in the content of −N + (CH 3 ) 3 group in the polymeric PVA matrix accelerates the transport of ions. The −N + (CH 3 ) 3 groups are beneficial for anion transport, allowing Cl − ion diffusion in the membrane. Therefore, the available H + and Fe 2+ cations also cross the membrane from feed side to dialysate side in order to meet the electrically neutral requirements. H + ions are transported much more extensively compared to Fe 2+ ion due to their small size and lower valence state [56,57].

Acid Recovery Performance of QDAB AEMs via Diffusion Dialysis (DD)
Acidic waste solutions mostly contain metal ions and inorganic acid, which is usually generated during different industrial processes such as metal electrolysis and metallurgical and acid cleaning processes [10]. Therefore, to analyze the DD performance properties for acid recovery, QDAB AEMs were employed to separate a HCl/FeCl2 aqueous solution (1 M HCl/0.25 M FeCl2) used as a model aqueous waste feed to assess their potential for application in acid recovery. The DD results of AEMs with different wt. % of QDAB in the PVA matrix in terms of acid dialysis coefficients (UH), separation factor (S,) and dialysis coefficient ferrous ion (UFe) at 25 °C are shown in Figure 7.
As shown in Figure 7, the acid dialysis coefficients (UH) values of QDAB AEMs increased rapidly by increasing the content of QDAB, which was attributed to −N + (CH3)3 It has been observed that the U Fe values increased from the membrane QDAB-30 to the QDAB-70. This was due to the higher water uptake and IEC value of the QDAB-70 membrane. A high water uptake of QDAB membranes is also beneficial for the free movement of ions through the membrane matrix that results in the transport of more Fe 2+ ions. A higher IEC facilitates the transport of counter anions through the ion exchange sites [58]. Hence, the increasing trend of U H and U Fe from QDAB-30 to QDAB-70 agrees well with the increase of IEC and of the water uptake values.
It has been observed that the UFe values increased from the membrane QDAB-30 to the QDAB-70. This was due to the higher water uptake and IEC value of the QDAB-70 membrane. A high water uptake of QDAB membranes is also beneficial for the free movement of ions through the membrane matrix that results in the transport of more Fe 2+ ions. A higher IEC facilitates the transport of counter anions through the ion exchange sites [58]. Hence, the increasing trend of UH and UFe from QDAB-30 to QDAB-70 agrees well with the increase of IEC and of the water uptake values. The separation factor is the ratio between UH and UFe, which indicates the difference in transport rates between H + and Fe 2+ ions. The obtained separation factor values were in the range of 24.7-41.4 and were greater than the reported value of hybrid PVA-SiO2 membranes (15.9-21) at 25 °C [32] and of commercial DF-120 AEMs having an S value of 18.5 [34]. The higher separation factor values are credited to the amplified selective interaction between the H + ions and AEMs.
The S values decreased gradually from the membrane QDAB-30 to the QDAB-70. This decrease was mainly due to the increase of IEC and water uptake in the presence of a higher QDAB content, resulting in the freel passing of H + and Fe 2+ ions through the membrane without much resistance by Cl − . This unrestricted transport of Fe 2+ ions is not favorable for membrane selectivity [7]. There is usually a trade-off between UH and selectivity. For example, QDAB-30 AEM showed the highest S value of 41.4, while it exhibited the lowest UH of 0.0186 m/h, while QDAB-70 showed the lowest selectivity (S = 24.7) and the highest UH value (0.0295 m/h).
In Table 3, we compared our results about acid recovery with those reported in the literature for AEMs. From the comparison, it can be easily seen that the prepared QDAB AEMs perform better than or comparably to many other reported membranes and have potential for acid recovery applications in the industry. The separation factor is the ratio between U H and U Fe , which indicates the difference in transport rates between H + and Fe 2+ ions. The obtained separation factor values were in the range of 24.7-41.4 and were greater than the reported value of hybrid PVA-SiO 2 membranes (15.9-21) at 25 • C [32] and of commercial DF-120 AEMs having an S value of 18.5 [34]. The higher separation factor values are credited to the amplified selective interaction between the H + ions and AEMs.
The S values decreased gradually from the membrane QDAB-30 to the QDAB-70. This decrease was mainly due to the increase of IEC and water uptake in the presence of a higher QDAB content, resulting in the freel passing of H + and Fe 2+ ions through the membrane without much resistance by Cl − . This unrestricted transport of Fe 2+ ions is not favorable for membrane selectivity [7]. There is usually a trade-off between U H and selectivity. For example, QDAB-30 AEM showed the highest S value of 41.4, while it exhibited the lowest U H of 0.0186 m/h, while QDAB-70 showed the lowest selectivity (S = 24.7) and the highest U H value (0.0295 m/h).
In Table 3, we compared our results about acid recovery with those reported in the literature for AEMs. From the comparison, it can be easily seen that the prepared QDAB AEMs perform better than or comparably to many other reported membranes and have potential for acid recovery applications in the industry. Table 3. Comparison of the DD performance of the membranes described in this work with that of membranes published in the literature using the HCl/FeCl 2 system at 25 • C.

Conclusions
In this work, novel hybrid AEMs were successfully synthesized with PVA, TEOS, and varying quantities of QDAB, from 30 to 70 wt. %, by the sol-gel reaction. The FTIR spectra confirmed the successful cross-linking of QDAB with PVA. IEC increased from 0.86 to 1.46 mmol/g, water uptake increased from 71.3-147.8%, and linear expansion ratio augmented from 28.7 to 39.5% with the increase of QDAB content in the membrane matrix. TGA analysis indicated that the membranes have good thermal stability. The tensile strength was 26.1-41.7 MPa, and flexibility values varied from 68.2% to 204.6%. SEM analysis showed that the membrane surface was compact and dense. The U OH values increased from 0.0186 to 0.0295 m/h, while the S values decreased from 41.4 to 24.7 with the increase of the content of QDAB. QDAB/PVA hybrid AEMs showed high proton permeability and selectivity compared to the commercial DF-120 AEM. The prepared AEMs have great potential for application in DD for acid recovery from industrial wastewater.