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Membrane-based separation processes have been used extensively for drinking water purification, wastewater treatment, and numerous other applications. More recent developments in membrane functionalization have made the use of membrane science important in diverse fields, from tunable separations to catalysis. The focus of this work is to create a common membrane platform for the incorporation of technologies capable of degrading target pollutants. Functionalized membranes capable of metal capture were created using water-based and solvent-based acrylic acid polymerization to synthesize poly (acrylic acid) (PAA) within poly(vinylidene fluoride) (PVDF) membrane pores. The COO− groups of PAA were used to capture Fe(II), which was then either reduced and doped with Pd to form Fe/Pd nanoparticles or used as-is for free radical generation with hydrogen peroxide. Fe/Pd nanoparticles were synthesized within the pores of a PAA/PVDF membrane functionalized via aqueous (green) chemistry and used to dechlorinate trichloroethylene (TCE) and 2,2′-dichlorobiphenyl (DiCB). A PAA/PVDF membrane containing immobilized Fe(III) was used to obtain controlled free radical generation and target organic (pentachlorophenol) degradation within the membrane pore under convective flow conditions.
The field of membrane separation is in a state of a tremendous growth and innovation. Membranes are essential for applications ranging from drinking water purification and wastewater treatment to pharmaceuticals production, food and beverage processing, medical devices, and separations needed for manufacturing chemicals, electronics, and a variety of other products (1–4). New processes are being reported frequently, and existing processes are also being constantly improved in order to enhance their competitiveness (5–7).
Conventional membranes are considered to be a separation media based solely on size (MF, UF), charge and/or size (NF). or solubility (RO, PV)) of species. However, with the advancement of functionalization chemistry and the availability of novel materials, further versatility can be obtained in the form of functionalized membranes. Functionalized membranes can be tailor-made to impart the desired functionality by a variety of active groups/molecules/moieties, depending on the applications. Membrane functionalization can be used to enhance separation capabilities (i.e., affinity, tunable separations) and extend the spectrum of applications towards new areas, such as designing drug delivery systems (by controlled, tunable solute transport), catalysis, or biocatalysis. A large variety of ligands have been used for membrane functionalization, the most common being polymers, amonoacids/polyaminoacids, metal affinity, ion exchange, etc. (8,9). Among these, membrane modification with ion exchange ligands has received extensive attention in a variety of processes and applications including nanofiltration (10,11), enzyme immobilization, and biocatalysis (12,13), catalysis (14,15), and heavy metal capture (16–20). An overview of membrane functionalization techniques and processes is shown in Fig. 1.
Our research group is involved in creating reactive membranes by functionalization with polyligands containing ion exchange groups (i.e., poly(acrylic acid) (PAA)). In particular, our focus is on metal (iron) ion capture and their use in oxidative and reductive reactions for the degradation of toxic organics such as trichloroethylene (TCE), 2,2′-dichlorobiphenyl (DiCB), or pentachlorophenol (PCP). The oxidative pathway, also known as the Fenton reaction, involves the generation of free radicals via the reaction of Fe(II) and H2O2. The reductive pathway utilizes metal nanoparticle formation within the membrane domain for catalytic dechlorination of the organic chlorinated compounds. Traditionally, the synthesis of nanoparticles and the application of the Fenton reaction have been performed in the solution phase. However, there are several advantages to immobilizing these metal species within a membrane domain.
There are several methods of PAA functionalization on membranes, as shown in Fig. 2. Various membranes can be used as platforms (supports) for PAA functionalization, but should have suitable thermal and chemical stability for the desired application. The simplest method is dipping the membrane in a PAA solution. The PAA diffuses inside the membrane pores and the chains are cross-linked by ethylene glycol (EG) to prevent leaching from the membrane. However, it was shown that PAA is coated primarily on the external membrane surface and at the pore mouth, thus blocking the PAA diffusion inside (21). This method does not take advantage of the internal membrane surface, and dramatically reduces the membrane pore size.
Another approach is to polymerize the monomer, acrylic acid, inside the membrane pores. This can be obtained by either surface-initiated or in situ polymerization. In the first case, initiator groups are immobilized on the membrane and the polymerization occurs via a radical transfer mechanism after the addition of the monomer (22). In the second case, the membrane is soaked in polymerization solution containing the initiator, the monomer, and the cross-linking agent. This solution diffuses inside the membrane pores and random polymerization occurs by heating the membrane (23,24).
An additional method of PAA immobilization on membrane supports is by forming polyelectrolyte layer-by-layer (LbL) assemblies via alternating adsorption of polycations and polyanions. Thus, thin films containing oppositely charged polyelectrolytes are formed on the external membrane surface (15,25,26).
Objectives of this research include:
All chemicals used were of reagent grade. TCE, ferrous sulfate, sodium citrate, sodium phosphate, hydrogen peroxide (30 wt%), pentane, sodium hydroxide, sulfuric acid, acetonitrile (HPLC-grade), and deionized ultra-filtered (DIUF) water were all purchased from Fisher Scientific. Copper(II) sulfate and potassium persulfate were purchased from EM Science. Toluene, acrylic acid, trimethylolpropane triacrylate (TMPTA), benzoyl peroxide, 3-(2-pyridyl)-5,6-diphenyl-1,2,4;-triazine-4′,4″-disulfonic acid sodium salt (ferrozine), 2,9-dimethyl-l,10-phenanthroline (DMP), PCP, 1,2-dibromoethane (EDB), and potassium tetrachloropalladate (II) were purchased from Sigma-Aldrich. Chloride reference solution (1000ppm) was purchased from Thermo Electron Corporation. Sodium nitrate was purchased from LabChem Inc., ethylene glycol was purchased from Mallinckrodt, and naphthalene-d8 and DiCB were purchased from Ultra Scientific. PVDF microfiltration membranes, both hydrophobic (HVHP) and hydrophilic (GVWP), with a thickness of 125 µm and nominal pore sizes of 450 nm and 220 nm, respectively, were obtained from Millipore Corporation.
PVDF membranes were coated with PAA by in situ polymerization of acrylic acid. Although various membrane materials can be used for this application, PVDF was chosen for its high chemical and thermal stabilities. The polymerization reaction was carried out in aqueous and organic (toluene) phases. In the organic phase, the polymerization solution containing 70 wt% toluene (solvent), 30 wt% acrylic acid (monomer), 1.2 wt% TMPTA (cross-linker), and 0.5 wt% benzoyl peroxide (initiator) was mixed for 30 min in a closed vessel. The procedure was described in detail previously (23,24).
Aqueous phase in situ polymerization of acrylic acid (green chemistry) was adapted from literature (27,28). The polymerization solution contained 30 wt% acrylic acid (monomer), ethylene glycol (cross-linker, added in a 1:10 molar ratio of EG to acrylic acid), and 1 wt% potassium persulfate (initiator). Each ethylene glycol molecule binds to two −COOH groups thus preventing PAA leaching from the membrane. However, the amount of cross-linking agent has to be kept low in order to maintain free −COOH groups for ion exchange. Under our experimental conditions, about 80% of the −COOH groups are free assuming one molecule of EG binds to two −COOH groups.
For both aqueous-based and solvent-based polymerization, a PVDF membrane was dipped in the polymerization solution for 2 minutes, sandwiched between 2 teflon plates, and placed in an oven at 90°C for 4 hours. Nitrogen gas was continuously supplied to remove oxygen, which acts as an inhibitor for the polymerization reaction. In order to ensure the proper wetting, hydrophobic PVDF membranes were used for solvent-phase polymerization and hydrophilized ones for the aqueous-phase polymerization.
The flowchart for membrane functionalization and nanoparticle synthesis is shown in Fig. 3. Prior to Fe2+ ion exchange, PAA-coated PVDF membranes were immersed in NaCl (20%wt) solution at pH 10 for 10 hours to convert the −COOH to –COONa form. The purpose was to minimize the pH effects on ion exchange equilibrium, thus enhancing the ion exchange capacity. In the next step, the membrane was washed with DIUF until the pH of the washing solution became neutral. Then, the membrane was immersed in FeCl2 solution (typically 180 mg/L Fe2+) at a pH of 5.5 for 4 hours. Nitrogen gas was bubbled to minimize Fe2+ oxidation. The reduction with NaBH4 ensured Fe nanoparticle formation and the membranes were stored in ethanol to prevent oxidation. The secondary metal, Pd, was deposited on the Fe nanoparticles by immersing the membrane in a K2PdCl4 solution containing ethanol/water (90:10 vol% mixture), preventing the oxidation of the highly reactive Fe nanoparticles. This created core-shell nanoparticles. The membranes were stored in ethanol until dechlorination reactions were carried out. Batch experiments were performed using either TCE or DiCB in order to determine the reactivity of the immobilized Fe/Pd nanoparticles.
Surface morphology of the bare, PAA-coated and nanoparticle-modified membranes were examined by Scanning Electron Microscopy instrument, Hitachi S-3200. This instrument was coupled with an X-ray energy dispersive (EDS) apparatus, which was used for membrane elemental analysis.
The Fourier Transform Infrared spectra of the bare and PAA-coated PVDF membranes were recorded on a Varian 7000e FTIR with attenuated total reflectance (ATR). Membranes were dried at 90°C for four hours before testing. Data was collected using 128 scans at a resolution of 4 cm−1.
Pd containing feed and permeate probes were quantified by Atomic Absorption Spectroscopy (AAS) using a Varian SpectrAA 220 Fast Sequential atomic absorption spectrometer at a wavelength of 246.6nm. The linear calibration range is between 0.2 and 28mg/L Pd. The error of analysis was <2%. The material balance was used to determine the amount of Pd deposited as a secondary metal on the membrane.
The amount of Fe captured during ion exchange was quantified using a Varian SpectrAA 220 Fast Sequential atomic absorption spectrometer equipped with a Fisher Scientific Fe data-coded hollow cathode lamp. The lamp was operated at a wavelength of 386.0 nm. The calibration curve was created using 7 different concentrations of Fe ranging from 90 to 900 µmol/L with R2 = 0.9993 and average analytical error of 1.3%.
The concentration of PCP was measured using a Shimadzu HPLC with photodiode array detector and a Premier C18 5µm 250mm × 4.6mm column. The column was operated under isocratic flow conditions of 0.6mL/min acetonitrile and 0.2mL/min water. The calibration curve was created using 9 different quantities of PCP ranging from 0.05 to 2.5 nmol with R2 = 0.9998 and average analytical error of 2.5%.
Dechlorination of TCE was conducted by cutting PAA/PVDF membranes containing Fe/Pd nanoparticles (original membranes were of 13.2cm2 external area and 125 µm thickness) into small pieces and immersing them in 20 mL sealed vials containing TCE solution. Probes were collected with a syringe at different times. TCE samples were extracted in pentane, and analyzed with a Hewlett Packard Series II 5890 GC-MS. In this analysis, the decrease of TCE concentration in time was monitored and EDB was used as an internal standard. The calibration was performed in between 5 and 120mg/L TCE, linear R2 = 0.9899, and the average analytical error was <8.5%.
Similar to the previous case, the dechlorination of dichlorobiphenyl was also conducted in 20 mL closed vials and probes being collected at different times. The samples extracted in hexane and analyzed with a Varian CP-3800 GC coupled with a Varian Saturn 2200 MS. The concentrations of the starting compound, DiCB, intermediate—chlorobiphenyl, and final product—biphenyl, were monitored with time.
In the linear range, between 1 and 25mg/L dichlorobiphenyl, the average analytical error was less than 2%.
The functionalization of the PVDF membranes with PAA was characterized by FTIR spectroscopy and stimuli-responsive water flux to pH. The chemical structures for the hydrophilized PVDF and PAA-coated PVDF membranes were studied by FTTR-ATR spectroscopy (Fig. 4). The PAA-coated PVDF membrane shows a distinct absorption band at 1710 cm−1, whereas the blank hydrophilic PVDF membrane does not. This band is due to the presence of C = O bond stretching in carboxylic acid groups, indicating successful PAA formation within the functionalized membrane. The strong absorption band at 1140–1280 cm−1 is characteristic of CF2 found in PVDF. Xu and Bhattacharyya (2008) performed both FTIR analysis and STEM-EDS mapping on hydrophobic PVDF membranes functionalized with PAA via the solvent-based method (23). FTIR data showed C = O bond stretching was present in the modified hydrophobic PVDF membranes, indicating successful PAA functionalization. This bond was not present in the blank hydrophobic PVDF membranes. STEM-EDS mapping indicated the presence of oxygen atoms, also confirming the formation of PAA.
With PAA present within the membrane pores, as indicated by FTIR, one would expect to see a stimuli-responsive water flux to pH. The effect of varying pH on water flux through the PAA/PVDF functionalized membrane is shown in Fig. 5. It can be seen that as the permeate pH is increased, the flux decreases, with a significant drop occurring between pH 3 and pH 6. This is in agreement with the findings of Hu and Dickson (2007), who conducted similar tests on PVDF membrane pores filled with PAA. Since the pKa of PAA is approximately 4.2, the PAA network will maintain a relatively neutral charge at a low pH, leaving it in a retracted state (13). As the pH is increased, more −COOH groups will become ionized, resulting in an elongation of the PAA network due to charge repulsion. While in the elongated state, there is significantly less core leakage and thus lower permeate flux than in the retracted state.
Based on weight gain, the amount of PAA deposited on the various membranes was estimated to be in the range of 3.5 to 4.5 mmol PAA/g dry membrane (4.1 to 4.9 mmol/cm3 membrane pore volume). Knowing the membrane thickness, the porosity, and the external surface area, the PAA gel occupies 28 to 39% of the membrane pore volume.
Fe/Pd bimetallic nanoparticles were synthesized within the membrane nanodomain, as described in Section titled “Membrane and Nanoparticle Characterization.” SEM imaging was used to examine the surface morphology for both bare and nanoparticle-modified PVDF membranes (Figs. 6a and b). The presence of spherical grains clearly indicates nanoparticle formation on the membrane surface. Higher resolution (100 k) imaging shows that there is a greater tendency for the particle agglomeration on the membrane surface (Fig. 7a), and the base particle size was estimated to be about 50 nm. Inside the membrane (Fig. 7b), there are more discreet particles with an approximate diameter of 50 nm. This reduced agglomeration as compared to the external surface is due to the fact that the chains are cross-linked and their mobility is reduced. The particle size can be modulated by changing the degree of cross-linking. At lower degrees of cross-linking, the particle size is expected to be higher since there is more chain mobility and adjacent nanoparticles can agglomerate, forming larger particles. For catalytic applications, smaller particles are preferred as they ensure a higher surface area and more accessibility to the active sites.
Elemental analysis of the modified membrane was performed by EDS (Fig. 8). From ion exchange principles, theoretically 1 mol of Fe2+ binds to two −COOH groups, yielding an Fe:O molar ration of 1:4. After reduction with NaBH4, Fe is replaced with Na+, resulting in 1 mol Na+ per −COOH group, yielding a Na:O molar ratio of 1:2. The results from EDS (Fe:Na:O molar ratio of 3.8:1.9:1) are close to the theoretical values (Fe:Na:O molar ratio of 4:2:1) showing that there is no physical metal adsorption on the membrane, only ion exchange.
As mentioned earlier, Fe/Pd-modified membranes were tested for dechlorination of two target toxic organic compounds: TCE and DiCB. The dechlorinaton results for the two toxic compounds performed with different membranes are shown in Figs. 9 and and10,10, respectively. The metal loading characteristics for the five membranes used in dechlorination studies are shown in Table 1.
The data in Figs. 9 and and1010 was fitted assuming a pseudo-first order rate law, and from a ln(C/C0) vs time plot, kobs, the observed pseudo-first order constant was determined. The surface-area-normalized rate constant, kSA (L/m2h), can be calculated from these kobs values using Eq. 1 where C0 is the initial concentration of the chlorinated compound, C is the concentration of the chlorinated compound at time t (h), aS is the specific surface area of the nanoparticles (m2/g), and ρm is the nanoparticle loading (g/L).
Assuming discreet spherical particles with a diameter of 50nm, as observed from SEM imaging, aS was calculated to be 15 m2/g. The nanoparticle loading was determined by dividing the amount of metal loaded on the membrane by the volume of the chlorinated solution (0.02 L). Based on these assumptions, the kSA value for each system was calculated, as shown in Table 1.
In a Fe/Pd bimetallic system, the role of Fe (reactant) in zero-valent form is to generate hydrogen via a corrosion reaction. Pd acts as a hydrogenation catalyst and thus can be considered as the active sites in the bimetallic system. From the data in Table 1, it can be observed that kSA value increases with the amount of Pd in bimetallic particles. Pd surface coverage can be estimated based on 50 nm particle size and Pd cross-sectional area of 0.0787 nm2 (31). For the five membranes used in the dechlorination experiments, Pd coverage was estimated to be in the range between 0.10 monolayers at the lowest Pd loading and 0.75 monolayers at the highest Pd loading. Since Pd coverage is less than 1 monolayer for all membranes, all Pd atoms are considered active sites, indicating the kSA value increases with increasing Pd loading. It is interesting to observe that the kSA value for membrane #5 (14.7 mg Fe/Pd, 2.6% wt Pd) is very similar (within 10%) to the one previously reported (24) under similar conditions (15 mg Fe loading, 2.3%wt Pd). For that case, the matrix for Fe/Pd nanoparticle formation was prepared using a different methodology, solvent-based acrylic acid polymerization.
Advanced oxidative techniques are commonly used for organic contaminant degradation. This includes the use of electrochemical, photolytic, and other free radical generating techniques (32). The generation of hydroxyl radicals via the reaction of ferrous iron and hydrogen peroxide was first proposed by Haber and Weiss in 1934 (Eq. 2) (33,34).
Hydroxyl radicals arc powerful oxidants which are highly unselective and capable of oxidizing both aliphatic and aromatic compounds (35). This reaction is autocatalytic and continues to propagate via Eqs. 3–7 until all hydrogen peroxide has been consumed (33,36,37).
The Fenton reaction is most efficient at a low pH, where the consumption of available Fe2+ is very rapid. The reduction of Fe3+ is much slower than the oxidation of Fe2+ and therefore becomes the rate-limiting step in the catalytic cycle once most of the Fe2+ has been converted to Fe3+. Several investigators have opted to use Fe(III) to initialize the decomposition of hydrogen peroxide instead of Fe(II) in order to promote the generation of other radical species (HO2• and O2•−) for use in degrading contaminants that are less susceptible to attack by OH• (38).
The Fenton reaction is much less efficient at near-neutral pH: in aerobic environments, Fe(II) is rapidly oxidized to Fe(III) which precipitates as Fe(OH)3, preventing its reduction to Fe(II), thus terminating the catalytic cycle. Much work has been done towards modifying the Fenton reaction so as to avoid these problems through the addition of a chelating agent (39,40). A chelate present in solution binds with the iron species, greatly reducing the rate of Fe(II) oxidation and eliminating the precipitation of Fe(III) as Fe(OH)3 at near-neutral pH. The advantages of iron chelation in the aqueous phase can be applied to the membrane domain via the incorporation of ion exchange groups.
Significant quantities of hydrogen peroxide are needed for practical applications, requiring the dilution of concentrated solutions; however, highly concentrated hydrogen peroxide can be hazardous to transport. Our group has developed a technique for the enzymatic production of hydrogen peroxide within the membrane domain (12,13,41). Glucose oxidase (GOX) is a well-known and robust enzyme which catalyzes the reaction of glucose and O2 to form hydrogen peroxide and gluconic acid at room temperature. GOX was electrostatically immobilized in a LbL assembly and glucose solution was passed through the membrane. Kinetic studies indicated there was minimal reduction in GOX activity (10 ± 5%) due to immobilization (13). Such a platform could be easily implemented for on-site hydrogen peroxide generation therefore avoiding the need to transport of concentrated solutions.
Ion exchange groups immobilized within membrane pores have been used for a variety of applications involving metal capture. Several investigators have utilized Nafion membranes for the immobilization of Fe(II)/Fe(III) and subsequent reaction with H2O2. Espro et al. (2000, 2001) (42,43) applied an Fe(II)-H2O2 Fenton system at elevated temperature and pressure for the oxidation of light alkanes. Fernandez et al. (2003) used a photoassisted Fe(III)-H2O2, system for the oxidation of target organics (44). Parra et al. (2004). utilized a similar photoassisted Fenton reaction for the oxidation of 4-chlorophenol (45).
The relative amounts of Fe(II) and Fe(III) present within the membrane domain determine the rate at which H2O2 is decomposed. The conversion of Fe(II) to Fe(III) within the PAA-filled pours was investigated by passing a solution containing 150 µmol/L H2O2 through the membrane via convection. As the H2O2 permeated, Fe(II) was gradually converted to Fe(III), until only Fe(III) remained, as seen in Fig. 11. No iron was released during H2O2 permeation. It is important to note that in solutions at pH = 6, soluble Fe(III) is not present as Fe3+, but mainly as Fe(OH)2+ and Fe(OH)3,aq. Because of this, COO-Fe(III) complexes may also be hydroxylated within the PAA domain. Until all iron is present as Fe(III), the rate of H2O2 decomposition will not reach a steady state since the apparent concentrations of the iron species are constantly changing. This is because the reaction of Fe(III) with H2O2 and/or radical species becomes the rate-limiting step.
For steady state experimentation, Fe(III) was not directly loaded into the membrane since it would precipitate at the pH required to obtain significant loading (above the pKa of PAA). Therefore, 22 µmol of Fe(II) were loaded into the membrane (external area =33.2cm2, thickness = 125 µm) and oxidized with a solution containing H2O2 until complete conversion to Fe(III) was achieved. Hydrogen peroxide solutions at varying concentrations and residence times were then permeated through the membrane. Figure 12 shows the conversion of H2O2 as a function of residence time at pH = 6. Residence time was varied by changing ΔP. Assuming the membrane behaved as a continuous stirred-tank reactor and the decomposition of H2O2 was fast-order, the fast-order rate constant, kCSTR, was calculated to be (7.8 ± 0.8) × 10−3 s−1 (shown in Fig. 12) using Eq. 8, where [H2O2]0 is the feed concentration of H2O2, [H2O2] is the permeate concentration of H2O2, τ is the residence time, and rH2O2 is the rate of H2O2 decomposition. Assuming [Fe(III)] is constant, the second-order rate constant, k’CSTR was found to be (8.1 ± 0.7) × 10−2 M−1 s−1 (Eq. 9).
The calculated value is approximately 40 times greater than k3. This is in agreement with the investigations of (46), who found the rate of azo-dye degradation in a photo-assisted Fenton reaction immobilized in a Nafion membrane was similar to that of a homogeneous reaction with approximately 100 times more Fe3+. It has been reported that Fe-carboxylate complexes on the surface of the membrane could be responsible for this reactivity (44). These complexes may also be responsible for the stability of PAA in the presence of free radicals (44).
Pentachlorophenol (PCP) was once a widely used fungicide for wood preservation that was banned from use in 1987. It is a toxic compound that can still be found in soils at several sites of wood preserving industries. PCP degradation via reaction with free radicals has been conducted, but most studies have been performed either with the assistance of UV light (photo-Fenton) (47,48) or at high temperature (49). Liou et al. used a Fe3+-resin system to oxidize PCP in solution at elevated temperatures, achieving over 90% degradation. Fukushima and Tatsumi (2001) achieved greater than 90% removal of PCP after 300 min of UV-irradiation in a H2O2/Fe(III)/humic acid system (47).
By permeating a solution containing 150 µmol/L H2O2 and 20 µmol/L PCP through a PAA/PVDF membrane containing immobilized Fe(III), PCP was degraded at initial pH = 6 and 25°C temperature (Fig. 13). The conversions of H2O2 and PCP were 24% ± 2% and 27% ± 2% (5.4 µmol/L), respectively, for a residence time of 60 ± 2 s. This corresponded to 7.1 mol H2O2 consumed/mol PCP degraded. These conversions can be adjusted by varying the amount of iron loading, residence time, and/or the pH. This degradation of PCP is greater than the ~5% (~2.5 µmol/L) results previously reported by (50) using solution-phase Fe(III)-H2O2 reactions (with higher H2O2 concentration) at pH = 5.
H2O2 conversion for the solutions containing PCP was lower than those containing no PCP, as seen in Fig. 12. This is to be expected since PCP acts as a scavenger of hydroxyl radicals, lowering the rate of Equation 6 and therefore the rate of H2O2 decomposition.
Functionalization of PVDF membranes with PAA was achieved using water and solvent-based acrylic acid polymerization methods. These membranes were stimuli-responsive, the flux through which was successfully controlled by varying the pH of the feed. The negatively charged ion exchange groups within the membrane pores were used to capture ferrous iron. These membranes were then employed to degrade target compounds using reductive and oxidative strategies. For the reductive approach, the immobilized Fe2+ was reduced to Fe0 and subsequently doped with Pd. This resulted in the formation of bimetallic (Fe/Pd) nanoparticles with an average size of 50 nm inside of the membrane pores. Particle aggregation was present only on the membrane surface and not within the membrane pores. The dependence of Fe/Pd-modified membrane reactivity created using water-based acrylic acid polymerization on Pd loading was established for the dechlorination of two model compounds, TCE and DiCB. Complete dechlorination of DiCB was obtained within 4h. The surface-area-normalized rate constant for reaction with dichlorobiphenyl was within 10% of the values previously reported using solvent-based methods for PAA/PVDF functionalization. For the oxidative approach, the conversion of Fe(II) to Fe(III) within the PAA/PVDF domain was quantified. The observed rate constant for H2O2 degradation via reaction with immobilized Fe(III) as a function of residence time through the membrane was calculated from experimental data. The subsequent generation of hydroxyl radicals in the same system indicated a successful degradation of pentachlorophenol (PCP).
This research was supported by the NIEHS/SBRP (Grant number: P42ES007380) and NSF-IGERT programs. Alex Montague was supported by the NSF/REU program.