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Water SA

versión On-line ISSN 1816-7950
versión impresa ISSN 0378-4738

Water SA vol.46 no.1 Pretoria ene. 2020 



Synthesis of PES and PES/chitosan membranes for synthetic acid mine drainage treatment



Mathaba J Machodi; Michael O Daramola

School of Chemical and Metallurgical Engineering, Faculty of Engineering and the Built Environment, University of the Witwatersrand, Private Bag X3, Wits 2050, Johannesburg, South Africa





In this study, chitosan was synthesised from chitin and used to modify polyethersulphone (PES) membrane prepared by the phase inversion method. PES membrane was blended with various concentrations of chitosan to produce PES/0.5 wt% chitosan, PES/0.75 wt% chitosan and PES/1 wt% chitosan membranes. The membranes were tested for metal and sulphate removal from acid mine drainage (AMD). The fabricated membranes were characterised using scanning electron microscopy (SEM), contact angle analyser, Fourier transform infrared (FTIR), porosity determination and pure water flux measurements. Separation performance was conducted on a dead-end filtration cell and metal ions were determined by atomic absorption spectroscopy (AAS), and ultraviolet and visible (UV-vis) spectrophotometry was used for sulphates. Pure water flux of the pristine PES membrane increased from 102 Lm2h1 to 107 Lm2h1 and 133 Lm2h1 for PES/0.5 wt% and PES/0.75 wt%, respectively. Further addition of chitosan to 1 wt% created a dense structure on the membrane surface, thereby reducing the flux to 120 Lm2h1. The rejection of cations and sulphate ions significantly improved for chitosan-modified membranes due to the creation of adsorptive and/or repulsive sites on the chitosan biopolymer as a result of amine group protonation. The results reveal that chitosan has potential to improve performance of PES membranes as a hydrophilic agent during AMD treatment.

Keywords: polyethersulphone, acid mine drainage, chitin, membrane flux




The discharge of acidic wastewater from active and abandoned mines poses significant water quality and environmental problems globally (Larsson et al., 2018). During mining operations, sulphide-containing rocks such as pyrites (FeS2) get exposed to water, air and microbial activities, which makes them vulnerable to oxidation. Pyrite will react with oxygen and water to produce acidic discharge which acts as a leaching agent of toxic metals and trace elements available in the host rocks (Kefeni et al., 2018). Equations 1 to 4 show the formation of acid drainage in the presence of air (oxygen), water and bacteria (Bwapwa et al., 2017; Othman et al., 2017; Kaur et al., 2018). The pyrite (FeS2) oxidation releases hydrogen, sulphate and ferrous irons (Fe2+) (Eq. 1). Further oxidation of ferrous iron (Fe2+) releases ferric iron (Fe3+) (Eq. 2) which either acts as an oxidizing agent and oxidizes more pyrite (Eq. 3) or will precipitate as iron hydroxide (Fe(OH)3) (Eq. 4).

Membrane separation process (MSP) has been successfully applied to treat AMD due to the high salt and metal retention capacity of membranes (Ritchie and Bhattacharyya, 2002; Geise et al., 2010; Elimelech and Phillip, 2011; Daramola et al., 2015). Nanofiltration (NF) membrane is the most preferred because of its low required pressure and energy consumption, high selectivity and permeate flux. NF membranes which are intermediate membranes between ultrafiltration (UF) and reverse osmosis (RO) membranes have higher permitted flux compared to other pressure-driven membranes and can retain dissolved molecules with molecular weight greater than 200 to 300 gmol1, as well as inorganic ions through electrostatic interaction between membrane charge and the ions combined with size exclusion (Carvalho et al., 2011). Astudy by Aguiar et al. (2016) showed NF membranes to be more suitable for AMD treatment than RO which had high permeate flux and solute rejection. Most commercial NF membranes available in the market are constructed using polyethersulphone (PES) material prepared through phase inversion methods (Zhao et al., 2013).

A significant challenge confronting NF membrane application is fouling, which is caused by suspended or dissolved organic and/or inorganic matter migrating from the liquid phase and forming deposits on the membrane surface, at the pore openings or within the membrane matrix (Aguiar et al., 2016). For economically feasible operation, membrane fouling must be controlled since it reduces permeability, increases energy consumption and shortens membrane lifespan. Although membrane fouling is considered inevitable, the rate and extent is highly impacted by membrane properties, feed characteristics and operational conditions (Wei et al., 2010). Although PES and PES-based membranes have been widely used, the main disadvantage is related to its hydrophobic character (Zhao et al., 2013). Several studies reviewed by Van der Bruggen (2009) and Khulbe et al. (2010) indicate that hydrophobicity is directly related to fouling. Introducing materials with high anti-fouling properties improves performance of pure polymeric membranes. Addition of hydrophilic functional groups through common practices such as surface grafting (Rahimpour, 2011), coating (Reddy et al., 2003) or blending with hydrophilic polymers (Peyravi et al., 2012) or nanoparticles (Vatanpour et al., 2012; Ji et al., 2015) has been widely reported to modify polymeric membranes. A large number of amino (-NH2) and hydroxyl groups which can act as binding sites for contaminants, and additional features such as high hydrophilicity, high mechanical and chemical stability and charge density, make chitosan a suitable membrane modifier (Wan Ngaha et al., 2011). The reactive amino functional groups on the chitosan structure binds to almost all Group III and transition metals. In acidic medium, the amino group gets protonated and attracts metal anions through ion exchange and repels cations through electrostatic repulsion (Anirudhan and Rijith, 2012).

Despite the research efforts on the use of modifiers in membrane modification, application of chitosan as a membrane modifier for the treatment of AMD is not well studied. Therefore, the aim of this study was to synthesize polyethersulphone membranes modified with chitosan for AMD treatment.




Dimethyl sulfoxide (DMSO), polyethersulphone (PES) granules (3 mm), sodium hydroxide (NaOH), sulphuric acid (H2SO4) and metal sulphate salts were purchased from Sigma-Aldrich (Pty) Ltd, South Africa. The chemicals were analytical grade, and therefore were used without further purification. Deionized water was prepared in-house and had a pH of 6.89 and conductivity of 0.19 mScm1. The pH and conductivity were measured using a Metler Toledo dual meter (Sevenduo pH /conductivity meter with a Metler Toledo inLab Pro ISM pH electrode and inLab 738 ISM conductivity probe). Chitosan used in this study was synthesized from chitin that was obtained by processing seashells collected from Durban South Beach, Rutherford.

Model AMD

Synthetic AMD solution (Table 1) was prepared as per the characterized data obtained from Tutu et al. (2008) and the composition of mine-water collected from Randfontein (Black Reef Incline, 17 and 18 Winzes). Synthetic AMD solution was used to avoid competition between desired and undesired species present in real AMD. The AMD was prepared in 1 000 mL of water and the pH was adjusted with concentrated sulphuric acid to 3.2.



Production of chitosan and synthesis of membrane

Firstly, seashells were washed and boiled in water to remove any impurities before crushing and milled with milling rods into fine powder (chitin). The following steps were carried out in chronological order to extract chitosan from milled chitin powder, (i) deproteinization, (ii) demineralization and (iii) deacetylation. Deproteinization was carried out by treating chitin with 6% NaOH solution and demineralization using 6% HCl. The steps were carried out for 2 h at 60 °C on a heating plate equipped with a magnetic stirrer. The resulting chitin was filtered with a vacuum pump and washed with deionized water until neutral pH. Deacetylation was carried out with 40% NaOH at 120°C for 2 h. The deacetylated chitosan was washed with deionized water until neutral pH. The solid to liquid ratio for all processes was set at 1:20.

PES and modified PES membrane preparation

PES granules were dissolved in DMSO on a magnetic stirrer at room temperature measured at 26.8 °C. Chitosan was added at different concentrations (0, 0.5, 0.75 and 1 wt%) and stirred for 24 h to obtain a homogenous gel. Before casting, the casting solution was left at ambient conditions to remove any air bubbles for 24 h. The gel was cast on a glass plate with a casting knife at 250 µm thickness. The membranes were immersed in deionized water and left in a coagulation bath for 24 h to allow desorption of the solvent from the membrane. The membranes were heated in an oven at 60°C to evaporate any trapped water and/or solvent from the membrane.

PES and PES/chitosan membrane and chitosan characterization

Addition of modifying agents always affects surface morphology of polymeric membranes. As such, surface images of the fabricated membrane were obtained with scanning electron microscopy (SEM), (TESCAN Vega 3xmu) equipped with EDS (OXFORD Xmas) to investigate morphological changes. The surface chemical structure of the membranes was analysed using Fourier transform infrared spectroscopy (FTIR). The wettability of the membranes was investigated using Dataphysics Optical contact angle analyser (OCA 15 EC GOP). The produced chitosan was characterised with Fourier transform infrared spectroscopy (FTIR) to identify functional groups present. The infrared spectra were recorded at room temperature in the wavenumber range of 4 000 to 650 cm-1 using Perkin Elmer Spectrum. The particle size distribution of chitosan was determined using laser diffraction method (Malvern Mastersizer 2000 instrument).

Porosity determination and contact angle analysis

The overall membrane porosity was estimated gravimetrically using water swelling of the membrane via absorption as a criterion to obtain fractional free volume (porosity) within the membrane. Pieces of membranes were cut and immersed in distilled water for 24 h at room temperature. Then the wet membranes were taken and placed between two filter papers and weighed to achieve wet weight (Ww). Thereafter, the wet membranes were placed in an oven at 50°C for 2 h and weighed again (Wd). The bulk porosity was obtained using Eq. 5:

where A is the membrane effective area, ɭ is the thickness measured with a digital micrometer and dw is water density (0.998 gcm3). Three pieces of membrane were measured, and the resultant average was taken as a final value.

The wettability of the membranes was investigated using Dataphysics Optical contact angle analyser (OCA 15 EC GOP) to quantify the hydrophilic properties of the membranes. Relatively low contact angle is an indication of the enhanced hydrophilic property of the membranes whereas high contact angle indicates a hydrophobic character. Ten random measurements were taken at different places on the membrane surface and the average value was utilized. It has been extensively reported that membrane-water contact angle keeps changing with time after water is dropped on the membrane surface. This was attributed to the evaporative effect. Therefore, as recommended by Bolong et al. (2009), to avoid this evaporative effect, measurements in this study were conducted as quickly as possible (within less than 10 s).

Membrane performance evaluation

Membrane performance evaluation was conducted at room temperature using a dead-end filtration cell (Fig. 1) with a holding cell capacity of 300 mL and effective filtration area of 14.6 cm2. After the membrane was fixed, deionized water was passed through the membrane to pre-press and compact the membrane to ensure immersion of water. Pure water flux, J, (Lm2h1) was determined at ambient temperature by permeating deionized water through the membrane. Nitrogen was used as a pressuring gas during the tests. This was necessary to determine the initial/original flux of the membrane before evaluating with AMD. The water flux was obtained using Eq. 6:




where V (L) is the volume of permeated water, A (m2) is the effective membrane area and t (h) is the filtration time.

Synthetic AMD solution was fed through the filtration cell pressured with nitrogen gas to vary the feed pressure and filtrates were collected and analysed for metal ion content using atomic absorption spectroscopy (Thermo scientific ICE 3000 series). Sulphates were analysed using a UV-vis spectrophotometer following the United States Environmental Protection Agency Method 3754 (USEPA, 1983).

Metal ion rejection was determined using Eq. 7:

where R is the percentage rejection, Cfeed and Cpermeate (mgL1) are concentration of metal ion in the feed and permeate, respectively.



Membrane characterization

Scanning electron microscopy

Scanning electronic microscope images of both surface and cross-sections of the prepared membranes, used to evaluate the effect of chitosan concentration, are shown in Fig. 2. Since polymeric materials and membranes are nonconductive by nature, before mounting membrane samples onto the specimen they were exposed to carbon coating first. Additionally, before mounting them on the specimen, cross-section samples were quickly cryogenically fractured by hand after being immersed in liquid nitrogen for 10 min before carbon coating

The SEM images illustrated in Fig. 2 shed light on the surface morphology and surface porosity of the membranes and their corresponding cross-sectional view. The difference between PES membrane (Fig. 2(a)) and PES/chitosan membranes (Fig. 2(b-d) can be observed. Fig. 2(a) illustrates the surface morphology of PES support, with uniformly distributed pores. Comparing the images of PES/chitosan reveals a diminished number of pores relative to the PES membrane. This is due to the addition of hydrophilic chitosan particles. The dense structure of PES/chitosan is clearly seen in the SEM images. Increasing chitosan particles to 0.75 and 1 wt% resulted in a high viscous casting gel which reduced the rate of phase inversion and produced a denser and more compact membrane (Ghaemi et al., 2015).

During the phase inversion method, the cast film was immersed in a coagulation bath containing water. Therefore, hydrophilic membrane modifiers such as chitosan tend to accumulate on the membrane surface due to the high presence of hydroxyl and amino groups. The increasing hydrophilicity of the membrane is demonstrated by the water contact angle results for the membranes (Fig. 4). The contact angle of PES membrane reduced from 92° to 64°, 60° and 58° for PES/0.5 wt% chitosan, PES/0.75 wt% chitosan and PES/1 wt% chitosan membranes, respectively. Figure 3 indicates the particle size distribution of chitosan particles which were synthesised from chitin; a mean size of 112 nm was observed. The membranes were cast on a glass plate using a hand casting knife set at 250 µm thickness. The particle size distribution results show that the synthesized chitosan has acceptable dimensions to be added to the membrane without creating cracks within the membrane. The cross-section SEM images illustrate a typical asymmetric PES structure with a dense skin top layer and a porous sublayer with large pore wall thickness. Although surface morphology showed a denser surface after addition of chitosan, the cross-section images reveal a more porous sublayer and reduced pore wall thickness relative to unmodified PES membrane. Moreover, the skin layer thickness decreased with addition of chitosan particles up to 0.75 wt%. Further addition to 1 wt% chitosan increased pore wall thickness and caused a reduction in membrane porosity (Table 2). Although unmodified PES membrane has bigger pores, its hydrophobic character is responsible for the low water flux. Increasing chitosan content from 0.5 to 0.75 wt% caused an increase in sub-layer micro-voids in the pore sizes from 2.2 to 4.11 µm. Further addition of chitosan to 1 wt% reduced the pores to 3.7 µm and this justifies the decline in membrane permeability.







Fourier transform infrared

Figure 4 compares the IR spectra of PES membranes blended with chitosan (Fig. 4a, 4b and 4c) with that of bare PES membrane (Fig. 4d) to verify structural information. The PES/chitosan membranes were prepared by varying the chitosan concentration from 0.5 to 1% (w/w). No significant differences between PES and PES/chitosan membranes could be perceived. However, flux and rejection experiments showed that the PES and PES/chitosan membrane performances were different. Although the PES and PES/chitosan membranes all had similar spectral peaks, SEM (Fig. 2) results showed reduced surface porous structure and enlarged macro-voids and pores with addition of chitosan. These spectral similarities could be attributed to the properties of the PES basic structure. Spectra of the PES sample were verified and are shown in Fig. 4d. The identified peak at 621 cm-1 is attributed to the C-stretching and 880 cm-1 to the C=C stretching on the aromatic ring structure. The peaks at 1 150 cm-1, 1 239 cm-1 and 1 483 cm-1 could be attributed to the sulfonyl (O=S=O) group while the aromatic ether (C-O-C) group is represented by the peak at 1 296 cm-1. The sharp peak at 706 cm-1 indicates the C-S stretching. FTIR has been extensively used to characterize chemical composition on surface modification of PES-modified membranes (Zhao et al., 2013). PES chemical structure does not contain O-H groups, however a typical O-H stretching between 3 200 and 3 500 cm-1 was observed. The membrane was immersed in a coagulation bath containing deionized water to allow complete desorption, and heated in an oven at 60°C to evaporate any trapped water or solvent. It seemed that a small amount of water penetrated and remained within the porous structure. Similar conclusions have been reported in the literature (Belfer et al., 2000; Ghiggi et al., 2017).

Contact angle analysis

Figure 5 details the contact angle measurements of the membranes with varying chitosan content. Blending hydrophilic chitosan with PES membrane had a significant influence on the hydrophilicity of the membrane. It is clear that introduction of chitosan triggered a downward trend in contact angle. Addition of 0.5 wt% chitosan reduced the contact angle of the PES membrane from 92° to 63.6°. Further addition of chitosan to 0.75 wt% and 1 wt% reduced the contact angle to 60.8° and 58°, respectively. This reduction in contact angle could be explained by the enhancement of water transport through the membranes as a result of water molecules' interaction with the amide group of the hydrophilic chitosan through hydrogen bonding. This decrease in contact angle with increasing chitosan content affirms the influence of chitosan as an agent to enhance the membrane surface hydrophilicity. Although the membrane's hydrophilicity was increased by adding chitosan from 0 to 1 wt%, as seen on Fig. 7, water flux of PES membranes at 1 wt% (97 Lm2h1) chitosan content was lower than that at 0.75 wt% (121 Lm2h1). Membrane permeability is affected considerably by membrane porosity, hydrophilicity and surface roughness. The increase in chitosan content from 0.75 to 1 wt% resulted in a decrease in the effective pore size (fractional free volume) of the membrane, which reduced the porosity of the membrane. Furthermore, introducing chitosan as an additional hydrophilic agent improved the degree of hydrophilicity of the membranes as compared to the study conducted by Shockravi et al. (2017). Introduction of chitosan improved the degree of hydrophilicity of the membrane by 58%.







Membrane performance investigation

Membrane initial/original membrane flux

Figures 6 and 7 demonstrate initial water flux of the membrane against various chitosan concentrations (0, 0.5, 0.75 and 1 wt%). Table 2 provides information about the relation between the membrane porosity and the PWF. The membranes were pre-pressed with deionized water to ensure complete immersion of water in the membranes before analysis. The operating pressure was increased at an interval of 1 bar (105 Nm-2) (Fig. 6). When the pressure was increased from 4 bar to 5 bar (4 × 105 Nm-2 to 5 × 105 Nm-2), the membrane was ripped apart. This is because increasing the applied pressure across the membrane is associated with large shear stress forces which push water molecules through the membrane wall surface. Under high pressure, more wastewater will be treated in a shorter period with contaminants pushed through the membrane surface. Conversely, low applied pressure will result in reduced transmembrane pressure which may lead to accumulation of particles on the membrane surface wall, as necessitated by laminar flow (Cheng and Lin, 2004). It would be expected that high pressures will force adsorbed materials on the membrane surface to permeate through the membrane and reduce rejection. Contrary to this, studies have proven that increasing transmembrane pressure in nanofiltration and reverse osmosis membrane application promotes sorption of water molecules and eventually results in an increase in water flux through the membrane (Zhong et al., 2007). Consequently, separation tests were conducted at 4 bar to ensure maximum membrane flux during the tests.

Figure 7 illustrates the effect of chitosan concentration on permeate flux of the membranes at 4 bars when filtering AMD solution. Addition of 0.5 wt% of chitosan particles induced an increment in pure water flux (PWF) from 97 to 108 Lm2h1. When chitosan concentration was increased to 0.75 wt%, the PWF reached its highest value of 121 Lm2h1, which is about 20% more than the unmodified membrane. However, increasing the chitosan amount in the blend to 1 wt% caused a water flux decline to 116 Lm2h1, though the flux was still higher than that of PES membrane. This could be attributed to the fact that increasing the chitosan amount caused blockage of effective pore sizes of the membrane. Chitosan is more hydrophilic than PES membrane due to its numerous functional groups which favour sorption of water molecules on the membrane surface; hence increased water flux was realised with increasing chitosan concentration. As mentioned earlier, membrane porosity and hydrophilicity play a vital role in membrane permeability; the results show that membrane permeability was influenced positively by the hydrophilic nature of the membrane when chitosan amount was 0.75 wt%. As observed in Fig. 5, though the hydrophilicity of the membrane increased with addition of chitosan to 1 wt%, its bulk porosity declined to 66.0%, showing that porosity dominated and influenced permeability and hence the flux declined. Chitosan is a hydrophilic filler and its addition should enhance the hydrophilicity of the membrane, which was observed at the loading of 5 wt% and 0.75 wt%. However, when the loading was increased to 1 wt% the degree of hydrophilicity reduced (see Fig. 7). This indicates that optimal loading is necessary to achieve an optimal degree of hydrophilicity.

The membranes were modified with different amounts of chitosan (0, 0.5, 0.75 and 1 wt%) and Fig. 8 illustrates the rejection of selected constituents in the synthetic AMD. The feed and permeate temperature did not differ significantly, therefore, the effect of temperature on membrane performance was ignored. The observed trend showed that addition of chitosan into the PES membrane matrix improved metal ion rejection. Additionally, the rejection of cations (Fe2+, Mn2+, Mg2+ and Ca2+) was higher than the rejection of anions (SO42-). In membrane separation processes, not only does the filtration mechanism exhibit a rejection process, but membrane surface charge also plays a vital role. It is generally known that PES membranes exhibit negatively charged surfaces without chitosan; therefore, rejection of anions was due to repulsive forces between anions and the negatively charged membrane through the Donnan exclusion mechanism (Crespo et al., 2014). As such, cation removal was due to ion exchange with the negatively charged surface of the PES membrane.



The pH of the feed used in this test was 3.2. Consequently, the higher rejection of cations (Mn2+, Fe2+, Mg2+ and Ca2+) as compared to anions (SO42-) could be attributed to the dominance of the strong repulsive forces between the positively charged membranes and the metal ions. In acidic solutions, the amine groups on the chitosan attract protons to form quaternary amine groups which cause the membrane to be more positively charged. Cation removal would be due to the electrostatic repulsive forces generated by the positive membrane and the cations. Additionally, sulphate ion removal will be attributed to the electrostatic attraction between the positive membrane and the anions.

Amine groups on the chitosan structure remain uncharged at neutral pH and addition of chitosan into the PES membrane matrix cannot affect the surface charge of the PES membrane. However, filtration tests in this study were conducted at a pH of 3.2, which protonates amine groups on chitosan (Liu et al., 2013). It could be observed that anion rejection improved from 53% for pristine PES membrane to 62, 73 and 72% for PES/0.5 wt%, PES/0.75 wt% and PES/1 wt%, respectively. This improvement in the rejection of sulphate ions by modified PES membrane could be attributed to adsorption of sulphate ions by the positively charged sites created on the chitosan structure under acidic conditions. In addition to the membrane's sieving mechanism, the strong cation removal behaviour was also due to strong dominant electrostatic repulsive forces between the positively charged membrane surface and cations. Metal ion rejection by the pristine PES membranes was 52% (Fe2+), 63% (Mn2+), 65% (Mg2+) and 50% (Ca2+). Adding 0.5 wt% chitosan to the PES blend improved membrane rejection to 56%, 74%, 76% and 55% for Fe2+, Mn2+, Mg2+, Ca2+, respectively. The general observed trend is that rejection increased with increasing chitosan content from 0 to 0.75 wt%. This was due to introduction of more amine functional groups which when protonated repel the cations or attract anions. It is reported in literature that metal ions favour formation of metal complexes with OH- groups at higher pH, and membrane rejection favours metal complexes rather than metal ions (Al-Zoubi et al., 2010). As recorded earlier, pH of the feed solution was acidic; therefore it could be concluded that the cations were removed as metal ions. Furthermore, introducing more chitosan particles to 1 wt% reduced membrane flux and rejection. This could be caused by molecular entanglement and aggregation which forms a thick layer of chitosan and creates weaker pore walls with bigger pore sizes. This pore size enlargement creates free passage for the contaminants and leads to lower rejection. Table 3 presents a comparison of pristine PES membranes and PES membrane modified with chitosan and multi-walled carbon nanotubes for treatment of wastewater containing metals, salts and oil. The PES membrane modified with multi-walled carbon nanotubes (MWCNTs) was added to compare a different modifier. Additionally, oil- and salt-containing wastewater are also considered to enable comparison with a different contaminant to AMD.



In this study, polyethersulphone (PES) membrane was modified by introducing chitosan particles and tested for acid mine drainage treatment. The resulting membranes displayed improved pure water flux from 102 Lm2h1 for pristine PES membrane to 107 Lm2h1 and 133 Lm2h1 for PES/0.5 wt% and PES/ 0.75 wt%, respectively. Further chitosan addition to 1 wt% created a dense structure (as observed on SEM images) which had a negative effect on permeability, which reduce the pure water flux to 120 Lm2h1. An improved degree of hydrophilicity with the addition of chitosan as a hydrophilic agent was confirmed by contact angle analysis which revealed a downward trend with increasing chitosan content. The observed high cation rejection relative to anions affirmed strong electrostatic repulsion by the membrane. However, further investigations aimed at enhancing performance, and checking operational stability and anti-fouling properties of the membrane during AMD treatment are required. Nevertheless, the results reported in this study reveal potential application of PES membrane modified with chitosan in the treatment of AMD.



The authors would like to acknowledge the CHMT of Wits University and University of Johannesburg for providing resources required to fulfil the objectives of the study. The effort by colleagues who assisted with characterization and analysis of the membranes is highly appreciated. The work was supported financially by the National Research Foundation of South Africa.



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Michael O Daramola

Received: 14 March 2019
Accepted: 13 November 2019

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