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Keywords = fouling mitigation

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35 pages, 26525 KiB  
Review
Efficient Removal of PFASs Using Photocatalysis, Membrane Separation and Photocatalytic Membrane Reactors
by Nonhle Siphelele Neliswa Mabaso, Charmaine Sesethu Tshangana and Adolph Anga Muleja
Membranes 2024, 14(10), 217; https://doi.org/10.3390/membranes14100217 - 14 Oct 2024
Viewed by 452
Abstract
Perfluoroalkyl and polyfluoroalkyl substances (PFASs) are persistent compounds characterized by stable C−F bonds giving them high thermal and chemical stability. Numerous studies have highlighted the presence of PFASs in the environment, surface waters and animals and humans. Exposure to these chemicals has been [...] Read more.
Perfluoroalkyl and polyfluoroalkyl substances (PFASs) are persistent compounds characterized by stable C−F bonds giving them high thermal and chemical stability. Numerous studies have highlighted the presence of PFASs in the environment, surface waters and animals and humans. Exposure to these chemicals has been found to cause various health effects and has necessitated the need to develop methods to remove them from the environment. To date, the use of photocatalytic degradation and membrane separation to remove PFASs from water has been widely studied; however, these methods have drawbacks hindering them from being applied at full scale, including the recovery of the photocatalyst, uneven light distribution and membrane fouling. Therefore, to overcome some of these challenges, there has been research involving the coupling of photocatalysis and membrane separation to form photocatalytic membrane reactors which facilitate in the recovery of the photocatalyst, ensuring even light distribution and mitigating fouling. This review not only highlights recent advancements in the removal of PFASs using photocatalysis and membrane separation but also provides comprehensive information on the integration of photocatalysis and membrane separation to form photocatalytic membrane reactors. It emphasizes the performance of immobilized and slurry systems in PFAS removal while also addressing the associated challenges and offering recommendations for improvement. Factors influencing the performance of these methods will be comprehensively discussed, as well as the nanomaterials used for each technology. Additionally, knowledge gaps regarding the removal of PFASs using integrated photocatalytic membrane systems will be addressed, along with a comprehensive discussion on how these technologies can be applied in real-world applications. Full article
(This article belongs to the Section Membrane Applications for Water Treatment)
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Figure 1

Figure 1
<p>(<b>a</b>) Schematic representation of the efffect of light on photocatalytic degradation of PFOA (this work), (<b>b</b>) degradation of PFOA in pure water using UV irradiation, (<b>c</b>) pure water using VUV irradiation and (<b>d</b>) sewage water using UV and VUV irradiation (<b>b</b>–<b>d</b> reproduced with permission from Ref. [<a href="#B24-membranes-14-00217" class="html-bibr">24</a>]).</p>
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<p>Schematic representation of the (<b>a</b>) Effect of pH on photocatalyst’s surface charge (i) and interaction of anionic PFASs and photocatalyst’s surface at different pH values (ii) (this work). (<b>b</b>) Effect of pH on photocatalytic degradation of PFOA and (<b>c</b>) zeta potential of TiO<sub>2</sub> at various pH values (<b>b</b> and <b>c</b> reproduced with permission from Ref. [<a href="#B35-membranes-14-00217" class="html-bibr">35</a>]).</p>
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<p>The effect of solute concentration on the degradation efficiency of PFOA with (<b>a</b>) Pb-BFO/0.5%rGO (reproduced with permission from Ref. [<a href="#B32-membranes-14-00217" class="html-bibr">32</a>]. (<b>b</b>) duo functional tri-metallic-oxide (f-TMO) photocatalyst (reproduced with permission from Ref. [<a href="#B37-membranes-14-00217" class="html-bibr">37</a>]) and (<b>c</b>) BiOI@Bi<sub>5</sub>O<sub>7</sub>I heterojunction photocatalyst (reproduced with permission from Ref. [<a href="#B38-membranes-14-00217" class="html-bibr">38</a>]).</p>
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<p>Schematic representation (<b>a</b>) of the degradation efficiency of PFASs at low photocatalyst dosage(i), optimal dosage(ii) and high dosage (iii) (this work). (<b>b</b>) Degradation of PFOA at various photocatalyst dosages (reproduced with permission from Ref. [<a href="#B41-membranes-14-00217" class="html-bibr">41</a>]).</p>
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<p>Configuration showing adsorption of PFOA on (<b>a</b>) In<sub>2</sub>O<sub>3</sub> and (<b>b</b>) TiO<sub>2</sub>.</p>
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<p>(<b>a</b>) Degradation and (<b>b</b>) defluorination of PFOA using noble metal-doped TiO<sub>2</sub> ((<b>a</b>,<b>b</b>) reproduced with permission from Ref. [<a href="#B49-membranes-14-00217" class="html-bibr">49</a>]); (<b>c</b>) schematic representation of the electron trapping in metal-doped photocatalyst (this work).</p>
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<p>Factors affecting the removal of PFASs via membrane separation.</p>
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<p>Schematic representation of PFAS rejection efficiency in the presence of organic matter, illustrating (<b>a</b>) size exclusion and (<b>b</b>) electrostatic interactions. Black arrows indicate electrostatic exclusion between PFAS molecules and the membrane surface, as well as electrostatic shielding caused by the adsorption of cations in solution, which shields the membrane surface. (Reproduced with permission from Ref. [<a href="#B58-membranes-14-00217" class="html-bibr">58</a>]).</p>
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<p>Rejection of (<b>a</b>) PFCAs and (<b>b</b>) PFSAs using NF membrane in spiked AFFF and groundwater solutions (Reproduced with permission from Ref. [<a href="#B8-membranes-14-00217" class="html-bibr">8</a>]).</p>
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<p>(<b>a</b>) Rejection of PFOS with varying concentrations. (<b>b</b>) Influence of PFOS concentration on the Flux decay rate (F/F<sub>0</sub>): F<sub>0</sub> is the pure water flux; F is the flux at a specific moment in time. (Reproduced with permission from Ref. [<a href="#B62-membranes-14-00217" class="html-bibr">62</a>]).</p>
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<p>(<b>a</b>) Schematic representation of the accumulation of molecules on surface of membrane (this work). (<b>b</b>,<b>c</b>) Rejection and permeate fluxes of PFOA and PFBA at various operation pressures [<a href="#B57-membranes-14-00217" class="html-bibr">57</a>].</p>
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<p>(<b>a</b>) Influence of pH on rejection of PFOS. (<b>b</b>) Zeta potentials of PMIA membrane at various solution pHs (reproduced with permission from Ref. [<a href="#B62-membranes-14-00217" class="html-bibr">62</a>]).</p>
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<p>(<b>a</b>) Formation of CF<sub>3</sub>(CF<sub>2</sub>)<sub>7</sub>SO<sub>3</sub>Ca due to electrostatic interaction between Ca<sup>2+</sup> and negatively charged sulfonate group; (<b>b</b>) formation of CF<sub>3</sub>(CF<sub>2</sub>)<sub>7</sub>SO<sub>3</sub> −Ca− O<sub>3</sub>S(CF<sub>2</sub>)<sub>7</sub>CF<sub>3</sub> through linkage of two PFOS molecules to Ca<sup>2+</sup>.</p>
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<p>Schematic representation of the rejection proficiency of NF membrane for long- and short-chain PFASs (<b>a</b>), effect of organic matter and cations on rejection of long- and short-chain PFAS molecules (<b>b</b>) (this work) and (<b>c</b>) rejection proficiency of RO and NF membranes for long- and short-chain PFASs [<a href="#B57-membranes-14-00217" class="html-bibr">57</a>].</p>
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<p>Schematic representation on the interaction of PFASs with membrane with (<b>a</b>) hydrophobic and (<b>b</b>) hydrophilic surface.</p>
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<p>Schematic diagram showing the adsorption of PFOA onto polyamide barrier layer (<b>a</b>); electrostatic repulsion between polyamide barrier layer modified with carbonyl groups and PFOA (<b>b</b>).</p>
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<p>Schematic diagram showing the removal of PFOA using NF membrane–UV hybrid system.</p>
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<p>Flow diagram of NF/UV–sulphite pilot system for treatment of groundwater (reproduced with permission from Ref. [<a href="#B104-membranes-14-00217" class="html-bibr">104</a>]).</p>
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<p>Schematic representation of an immobilized photocatalytic membrane reactor with crossflow filtration system.</p>
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<p>A schematic diagram showing the photocatalytic degradation of PFOA adsorbed onto the photocatalytic membrane after exposure to UV.</p>
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16 pages, 3326 KiB  
Article
Typical Heterotrophic and Autotrophic Nitrogen Removal Process Coupled with Membrane Bioreactor: Comparison of Fouling Behavior and Characterization
by Qiushan Liu, Tong Zhou, Yuru Liu, Wenjun Wu, Yufei Wang, Guohan Liu, Na Wei, Guangshuo Yin and Jin Guo
Membranes 2024, 14(10), 214; https://doi.org/10.3390/membranes14100214 - 7 Oct 2024
Viewed by 708
Abstract
There is limited research on the relationship between membrane fouling and microbial metabolites in the nitrogen removal process coupled with membrane bioreactors (MBRs). In this study, we compared anoxic-oxic (AO) and partial nitritation–anammox (PNA), which were selected as representative heterotrophic and autotrophic biological [...] Read more.
There is limited research on the relationship between membrane fouling and microbial metabolites in the nitrogen removal process coupled with membrane bioreactors (MBRs). In this study, we compared anoxic-oxic (AO) and partial nitritation–anammox (PNA), which were selected as representative heterotrophic and autotrophic biological nitrogen removal–coupled MBR processes for their fouling behavior. At the same nitrogen loading rate of 100 mg/L and mixed liquor suspended solids (MLSS) concentration of 4000 mg/L, PNA-MBR exhibited more severe membrane fouling compared to AO-MBR, as evidenced by monitoring changes in transmembrane pressure (TMP). In the autotrophic nitrogen removal process, without added organic carbon, the supernatant of PNA-MBR had higher concentrations of protein, polysaccharides, and low-molecular-weight humic substances, leading to a rapid flux decline. Extracellular polymeric substances (EPS) extracted from suspended sludge and cake sludge in PNA-MBR also contributed to more severe membrane fouling than in AO-MBR. The EPS subfractions of PNA-MBR exhibited looser secondary structures in protein and stronger surface hydrophobicity, particularly in the cake sludge, which contained higher contents of humic substances with lower molecular weights. The higher abundances of Candidatus Brocadia and Chloroflexi in PNA-MBR could lead to the production of more hydrophobic organics and humic substances. Hydrophobic metabolism products as well as anammox bacteria were deposited on the hydrophobic membrane surface and formed serious fouling. Therefore, hydrophilic membrane modification is more urgently needed to mitigate membrane fouling when running PNA–MBR than AO–MBR. Full article
(This article belongs to the Section Membrane Applications for Water Treatment)
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Figure 1
<p>The concentration of NH<sub>4</sub><sup>+</sup>−N, NO<sub>2</sub><sup>−</sup>−N, and NO<sub>3</sub><sup>−</sup> − N in the influent and effluent of (<b>a</b>) AO−MBR and (<b>b</b>) PNA−MBR and the temporal variation in TMP during the operation of the two reactors (<b>c</b>).</p>
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<p>Fouling behavior and characterization of AO/PNA supernatant and effluent of AO/PNA−MBR. (<b>a</b>) Normalized flux transformation; (<b>b</b>) membrane resistance calculation; (<b>c</b>) protein and polysaccharide concentration; (<b>d</b>) total organic carbon (TOC) and UV<sub>254</sub>; (<b>e</b>) FTIR analysis; (<b>f</b>) MW distribution.</p>
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<p>Normalized flux transformation. (<b>a</b>,<b>b</b>) EPS extracted from the suspended sludge; (<b>c</b>,<b>d</b>) EPS extracted from the cake sludge.</p>
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<p>Contents and EEM analyses of SMP, LB-EPS, and TB-EPS in suspended sludge (<b>a</b>,<b>c</b>) and the cake sludge on day 44 (<b>b</b>,<b>d</b>) in the AO-MBR and PNA-MBR.</p>
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<p>Taxonomic distribution of the microbial community in the sludge of the AO-MBR and PNA-MBR in the operational phase (0 d and 44 d) of the suspended sludge and the cake sludge at phylum (<b>a</b>) and genus (<b>b</b>) level by 16S rRNA sequencing.</p>
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15 pages, 5791 KiB  
Article
Operational and Design Factors in Air Staging and Their Effects on Fouling from Biomass Combustion
by Akram Elsebaie, Mingming Zhu and Yasir M. Al-Abdeli
Sustainability 2024, 16(19), 8584; https://doi.org/10.3390/su16198584 - 3 Oct 2024
Viewed by 533
Abstract
The global transition towards a carbon-neutral economy highlights the potential of biomass as a renewable fuel source. However, the sustainability of biomass energy systems is challenged by its complex fouling behaviours during combustion. This study investigates the impact of air staging on mitigating [...] Read more.
The global transition towards a carbon-neutral economy highlights the potential of biomass as a renewable fuel source. However, the sustainability of biomass energy systems is challenged by its complex fouling behaviours during combustion. This study investigates the impact of air staging on mitigating fouling in biomass combustion. By optimising the secondary-to-total air flowrate ratio (Qs/Qt) and the positioning of secondary air, this research investigates the impact of operational and design parameters on fouling deposits in biomass combustion. A fixed-bed combustor was used for the experiments, with hardwood pellets as fuel. This study employed TGA and SEM to analyse the fouling deposit samples’ chemical composition and morphology. First, visible inspection established that the inclination of fouling matter to accumulate on cooled deposition pipes is indeed sensitive to Qs/Qt. The results show that lower Qs/Qt ratios (<0.50) lead to heavier, stickier fouling. Peak temperatures in the fuel bed increase with higher Qs/Qt, enhancing the combustion efficiency and affecting the fouling characteristics. SEM analysis further shows that higher Qs/Qt ratios produce finer, more dispersed fouling particles, whereas lower ratios result in larger, more cohesive particles. These findings provide actionable insights for enhancing the sustainability of biomass energy systems and minimising their environmental impact. Full article
(This article belongs to the Section Pollution Prevention, Mitigation and Sustainability)
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Figure 1
<p>(<b>a</b>) Combustor sectional view and (<b>b</b>) lab set-up: (1) primary air inlet ports (2×), (2) packed fuel bed, (3) fuel charging ports, (4) fouling module and air-cooled fouling deposition probes, (5) exhaust stack, (6) secondary air supply line and distribution, (7) thermocouples.</p>
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<p>(<b>a</b>) Fouling module lab set-up and (<b>b</b>) schematic diagram.</p>
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<p>Deposit pipes’ physical appearance: (<b>a</b>) Qs/Qt = 0.33 at LI = 200 mm, (<b>b</b>) Qs/Qt = 0.33 at LI = 300 mm, (<b>c</b>) Qs/Qt = 0.50 at LI = 200 mm, (<b>d</b>) Qs/Qt = 0.50 at LI = 300 mm, (<b>e</b>) Qs/Qt = 0.66 at LI = 200 mm, (<b>f</b>) Qs/Qt = 0.66 at LI = 300 mm, (<b>g</b>) Qs/Qt = 0.71 at LI = 200 mm, (<b>h</b>) Qs/Qt = 0.71 at LI = 300 mm, (<b>i</b>) Qs/Qt = 0.75 at LI = 200 mm, and (<b>j</b>) Qs/Qt = 0.75 at LI = 300 mm.</p>
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<p>Normalised weight loss percentages of fouling deposits derived from TGA (left <span class="html-italic">Y</span>-axis) at Qs/Qt = 0.33 to 0.75; program temperature (right <span class="html-italic">Y</span>-axis). Conditions: (<b>a</b>) LI = 200 mm and (<b>b</b>) LI = 300 mm.</p>
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<p>Temperatures, ash content, and total deposits for (<b>a</b>) LI = 200 mm and (<b>b</b>) LI = 300 mm at Qs/Qt = 0.33 to 0.75. Left axis: fuel bed temperatures (°C) and total fouling deposits (mg). Right axis: fouling probe temperatures.</p>
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<p>SEM images of fouling deposits samples for combustion condition LI = 200 mm at Qs/Qt ratios of (<b>a</b>) 0.33, (<b>b</b>) 0.50, (<b>c</b>) 0.66, (<b>d</b>) 0.71, and (<b>e</b>) 0.75.</p>
Full article ">Figure 6 Cont.
<p>SEM images of fouling deposits samples for combustion condition LI = 200 mm at Qs/Qt ratios of (<b>a</b>) 0.33, (<b>b</b>) 0.50, (<b>c</b>) 0.66, (<b>d</b>) 0.71, and (<b>e</b>) 0.75.</p>
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<p>(<b>a</b>) CO (100×) (ppm) and NOx (ppm) emissions and (<b>b</b>) CO<sub>2</sub>%, O<sub>2</sub>% (left axis), and burning rate (kg·m<sup>−2</sup>·s<sup>−1</sup>) (right axis) at LI = 200 mm (solid) and LI = 300 mm (stripes) for Qs/Qt = 0.33 to 0.75.</p>
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25 pages, 2286 KiB  
Review
Innovative Trends in Modified Membranes: A Mini Review of Applications and Challenges in the Food Sector
by Nicole Novelli do Nascimento, Carolina Moser Paraíso, Luiza C. A. Molina, Yuliya S. Dzyazko, Rosângela Bergamasco and Angélica Marquetotti Salcedo Vieira
Membranes 2024, 14(10), 209; https://doi.org/10.3390/membranes14100209 - 28 Sep 2024
Viewed by 525
Abstract
Membrane technologies play a pivotal role in various industrial sectors, including food processing. Membranes act as barriers, selectively allowing the passage of one or other types of species. The separation processes that involve them offer advantages such as continuity, energy efficiency, compactness of [...] Read more.
Membrane technologies play a pivotal role in various industrial sectors, including food processing. Membranes act as barriers, selectively allowing the passage of one or other types of species. The separation processes that involve them offer advantages such as continuity, energy efficiency, compactness of devices, operational simplicity, and minimal consumption of chemical reagents. The efficiency of membrane separation depends on various factors, such as morphology, composition, and process parameters. Fouling, a significant limitation in membrane processes, leads to a decline in performance over time. Anti-fouling strategies involve adjustments to process parameters or direct modifications to the membrane, aiming to enhance efficiency. Recent research has focused on mitigating fouling, particularly in the food industry, where complex organic streams pose challenges. Membrane processes address consumer demands for natural and healthy products, contributing to new formulations with antioxidant properties. These trends align with environmental concerns, emphasizing sustainable practices. Despite numerous works on membrane modification, a research gap exists, especially with regard to the application of modified membranes in the food industry. This review aims to systematize information on modified membranes, providing insights into their practical application. This comprehensive overview covers membrane modification methods, fouling mechanisms, and distinct applications in the food sector. This study highlights the potential of modified membranes for specific tasks in the food industry and encourages further research in this promising field. Full article
(This article belongs to the Section Membrane Applications for Other Areas)
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<p>Annual publications on modified membranes with application in food areas from 2016 to 2023. Bars and dashed line reflect annual growth through 2022 and decline in 2023 are highlighted.</p>
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<p>Keywords utilized in chosen articles and central countries whose authors published in the modified membrane field within the food sector between 2020 and 2024 are depicted: (<b>A</b>) keyword map indicating five points of similarity among articles; (<b>B</b>) collaboration network map among countries identified with a minimum of five citations.</p>
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<p>Application of pressure-driven membrane separation for removal of different species from liquids.</p>
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<p>Scheme of electrodialysis: The colored bars refer to the sequential arrangement of anodes and cathodes, incorporating cation exchange membranes (orange to green—concentrate) and anion exchange membranes (red to green—concentrate). When both ions are present, the bar is represented by blue—diluted.</p>
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<p>Scheme of membrane distillation: The different shapes represent solid compounds and/or microorganisms that may be present in the liquid. With the change in pressure during distillation, only vapor will pass through the hydrophobic membrane (blue circles).</p>
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<p>Tocopherol recovery in oil industry using modified membrane by [<a href="#B95-membranes-14-00209" class="html-bibr">95</a>].</p>
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23 pages, 7079 KiB  
Article
The Impact of pH on Fouling and Related Physicochemical Properties of Skim Milk Concentrate during Heat Treatment Using a Laboratory-Scale Fouling Rig
by Tara R. Murphy, Eoin W. Finnegan, Justyna Tarapata, Tom F. O’Callaghan and James A. O’Mahony
Foods 2024, 13(19), 3100; https://doi.org/10.3390/foods13193100 - 28 Sep 2024
Viewed by 489
Abstract
The objective of this study was to investigate the effect of pH (6.1, 6.3, 6.5, and 6.7) on heat-induced changes in concentrated skim milk as related to fouling in heat exchangers. Skim milk (30%, w/w, total solids) was recirculated in [...] Read more.
The objective of this study was to investigate the effect of pH (6.1, 6.3, 6.5, and 6.7) on heat-induced changes in concentrated skim milk as related to fouling in heat exchangers. Skim milk (30%, w/w, total solids) was recirculated in a laboratory-scale fouling rig at an initial target temperature of 85 °C for 90 min to simulate thermal processing and preheating of evaporated liquid concentrate feeds in dairy processing. This study investigated key changes in relevant physicochemical properties, such as viscosity, particle size, and sedimentation, as major contributors to fouling at lower pHs (6.1 and 6.3). Additionally, protein aggregation and calcium phosphate precipitation were identified as significant contributors to fouling deposits. Possible strategies to mitigate fouling were determined, including optimizing pH and adjusting heat treatment parameters to minimize protein denaturation and mineral deposition. The findings indicate that carefully controlling pH and processing parameters can greatly enhance the efficiency of milk concentration by evaporation and tailor finished product quality. Moreover, this study showed that monitoring of CIP solutions for protein content and turbidity provides valuable information on the intensity of fouling and the efficiency of cleaning. Full article
(This article belongs to the Section Dairy)
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<p>Process flow diagram of modified fouling rig set-up (<b>a</b>), the feed vessel from the modified fouling rig set-up (<b>b</b>), top-down view of the feed vessel from the modified fouling rig set-up, showing the feed tube designed to return product at an angle to promote turbulence without aeration or foaming (<b>c</b>). The shaded elements highlight the modifications compared to the set-up proposed by Hebishy et al. [<a href="#B21-foods-13-03100" class="html-bibr">21</a>].</p>
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<p>Heat coagulation time (HCT) at 120 °C as a function of pH for concentrated reconstituted skim milk at 30% total solids (TS) (■) and at 9% TS (□). Results are the means of data from three independent trials. <sup>A–F</sup> Mean values at 30% TS with different superscript letters are significantly different (<span class="html-italic">p</span> &lt; 0.05). <sup>a–d</sup> Mean values at 9% TS with different superscript letters are significantly different (<span class="html-italic">p</span> &lt; 0.05).</p>
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<p>pH (<b>A</b>) and conductivity (<b>B</b>) as a function of time of concentrated skim milk solutions (30% <span class="html-italic">w</span>/<span class="html-italic">w</span>, total solids) at a starting pH of 6.1 (<span style="color:#767171">●</span>), 6.3 (♦), 6.5 (<span style="color:#767171">▲</span>), and 6.7 (<span style="color:#767171">■</span>) during recirculation on the fouling rig at 85 °C. The temperature of the feed as a function of time (dashed line) is also shown. Results are the means of data from two independent trials. Error bars represent one standard deviation.</p>
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<p>Images of the surface of the heat exchanger outlet after recirculation of concentrated skim milk solutions at 30% <span class="html-italic">w</span>/<span class="html-italic">w</span> total solids at pH 6.1, 6.3, 6.5, and 6.7 at 85 °C for 90 min.</p>
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<p>Difference in temperature of heating medium and product as a function of recirculation time for concentrated skim milk solutions at 30% <span class="html-italic">w</span>/<span class="html-italic">w</span>, total solids at pH 6.1 (●), 6.3 (♦), 6.5 (▲), and pH 6.7 (■), after the initial 40 min heat-up time of the fouling experiment. Results are the means of data from two independent trials.</p>
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<p>Apparent viscosity at a shear rate of 300 s<sup>−1</sup> and 25 °C for concentrated skim milk solutions at 30% <span class="html-italic">w</span>/<span class="html-italic">w</span>, total solids, and pH 6.1, 6.3, 6.5, or 6.7 after 90 min of recirculation in the fouling rig at 85 °C. The unheated control was not subjected to heat treatment on the fouling rig. Results are the means of data from two independent trials. Mean values not sharing a common letter differ significantly (<span class="html-italic">p</span> &lt; 0.05).</p>
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<p>Particle size distribution of concentrated skim milk solutions at 30% (<span class="html-italic">w</span>/<span class="html-italic">w</span>) total solids after 90 min of recirculation in the fouling rig at 85 °C at pH 6.1, 6.3, 6.5, and 6.7 and unheated control.</p>
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<p>The relationship between pH and sediment formation following recirculation of concentrated skim milk solutions at 30% (<span class="html-italic">w</span>/<span class="html-italic">w</span>) total solids on the fouling rig at 85 °C for 90 min. The protein, ash, and moisture content of the sediments is expressed as a percentage of the total sediment formed for each sample. The unheated control was not subjected to any heat treatment. Results are the means of data from two independent trials. Mean values for sediment formation (%) with different superscript letters are significantly different (<span class="html-italic">p</span> &lt; 0.05).</p>
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<p>Protein content (<b>A</b>) and ash content (<b>B</b>) of cleaning solutions recovered after applying a cleaning-in-place protocol to the fouling rig after recirculation of concentrated skim milk solutions at 30% (<span class="html-italic">w</span>/<span class="html-italic">w</span>) total solids at 6.1 (<span style="color:#3366CC">■</span>), 6.3 (<span style="color:gray">■</span>), 6.5 (□), and 6.7 (<span style="color:#1F3864">■</span>) on the fouling rig at 85 °C for 2 h. Results are the means of data from two independent trials. Mean values within each individual cleaning step (i.e., water rinse) with different superscript letters are significantly different (<span class="html-italic">p</span> &lt; 0.05).</p>
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<p>Sodium dodecyl sulfate–polyacrylamide gel electrophoresis (SDS-PAGE) electrophoretograms of fouling material recovered from the heat exchanger of the fouling rig after recirculation of concentrated skim milk solutions at 30% <span class="html-italic">w</span>/<span class="html-italic">w</span> total solids at pH 6.1 and 6.3 at 85 °C for 90 min: lanes 1 and 10, molecular weight marker; lanes 2–3 and 6–7, foulant at pH 6.1; lanes 4–5 and 8–9, foulant at pH 6.3. Lines 1–5: reducing conditions; lines 6–10: non-reducing conditions.</p>
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19 pages, 2661 KiB  
Article
Enhanced Pollutant Removal and Antifouling in an Aerobic Ceramic Membrane Bioreactor with Bentonite for Pharmaceutical Wastewater Treatment
by Salaheddine Elmoutez, Hafida Ayyoub, Mohamed Chaker Necibi, Azzedine Elmidaoui and Mohamed Taky
Membranes 2024, 14(10), 205; https://doi.org/10.3390/membranes14100205 - 26 Sep 2024
Viewed by 557
Abstract
This study examined the impact of adding bentonite clay (concentration of 1.5 to 10 g/L) to a pilot-scale aerobic ceramic membrane bioreactor (AeCMBR) for treating pharmaceutical wastewater (PhWW). The hydraulic retention time (HRT) was maintained at 24 h; the dissolved oxygen was between [...] Read more.
This study examined the impact of adding bentonite clay (concentration of 1.5 to 10 g/L) to a pilot-scale aerobic ceramic membrane bioreactor (AeCMBR) for treating pharmaceutical wastewater (PhWW). The hydraulic retention time (HRT) was maintained at 24 h; the dissolved oxygen was between 2 mg/L (on) and 4 mg/L (off) throughout operation. Organic and nitrogen pollution removal rates and heavy metal (Cu, Ni, Pb, Zn) reduction rates were assessed. The chemical oxygen demand (COD) removal efficiency exceeded 82%. Adsorption improved ammonia (NH4+) removal to 78%; the addition of 5 g of bentonite resulted in a 38% improvement compared with the process without bentonite. The average nitrate concentration decreased from 169.69 mg/L to 43.72 mg/L. The average removal efficiencies for Cu, Ni, Pb and Zn were 86%, 68.52%, 46.90% and 56.76%, respectively. Bentonite at 5 g/L significantly reduced membrane fouling. The cost–benefit analysis enabled us to predict that the process will meet the multiple objectives of durability, treatment performance and economic viability. The combination of an AeCMBR and bentonite adsorption has proven to be a valuable solution for treating highly polluted wastewater. Full article
(This article belongs to the Topic Technologies for Wastewater and Sludge Treatment)
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<p>Schematic illustration of the AeCMBR pilot configuration.</p>
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<p>COD concentration in AeCMBR–bentonite supernatant and effluent.</p>
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<p>NH4+ removal performance of the AeCMBR–bentonite system.</p>
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<p>The variation in NO<sub>3</sub> removal during operation.</p>
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<p>Adsorption behaviors of (<b>a</b>) Cu, (<b>b</b>) Ni, (<b>c</b>) Pb, (<b>d</b>) Zn in the AeCMBR–bentonite system.</p>
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<p>Total membrane resistance as a function of bentonite concentration.</p>
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13 pages, 3229 KiB  
Article
Characterization of Silica Sand-Based Pervious Bricks and Their Performance under Stormwater Treatment
by Meijuan Chen, Weiying Li, Zhiqiang Dong and Dawei Zhang
Water 2024, 16(18), 2625; https://doi.org/10.3390/w16182625 - 16 Sep 2024
Viewed by 604
Abstract
The acceleration of urbanization has disrupted natural water cycles, resulting in increased impervious urban surfaces and non-point source pollution from stormwater runoff. Addressing urban stormwater recharge has become crucial. This study introduces a novel silica sand-based permeable filtration material, investigating its surface characteristics, [...] Read more.
The acceleration of urbanization has disrupted natural water cycles, resulting in increased impervious urban surfaces and non-point source pollution from stormwater runoff. Addressing urban stormwater recharge has become crucial. This study introduces a novel silica sand-based permeable filtration material, investigating its surface characteristics, pore structure, permeability, and pollutant interception capabilities. The results demonstrate that hydrophilic binder coating modification of the permeable surface sand aggregate, combined with hydrophilic inorganic additives, having a porous structure with an average pore size of less than 50 μm and a porosity between 15% and 35%, significantly enhances surface hydrophilicity, achieving a permeation rate of up to 6.8 mL/(min·cm²). Moreover, it shows exceptional filtration and anti-clogging properties, achieving over 98% suspended solids interception and strong resistance to fouling. Dynamic biofilm formation experiments using simulated rain and domestic wastewater explore biofilm morphology and function on silica sand filtration well surfaces. Mature biofilms sustain COD removal efficiency exceeding 70%, with levels consistently below 50 mg/L, NH4+ decreasing to 2 mg N/L, and total nitrogen maintained below 10 mg N/L. The system features anoxic, anoxic, and aerobic zones, fostering synergistic organic matter and nitrogen removal by diverse microorganisms, enhancing pollutant mitigation. Silica sand-based permeable filtration material effectively mitigates urban stormwater runoff pollutants—suspended solids, organic matter, and nitrogen—offering an innovative solution for sponge city development and rainwater resource management. Full article
(This article belongs to the Special Issue Urban Stormwater Harvesting, and Wastewater Treatment and Reuse)
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<p>(<b>A</b>) Original silica sand photo; (<b>B</b>) schematic diagram of sand grain coating modification; (<b>C</b>) photo of modified sand grains; (<b>D</b>) silica sand permeable and filter brick; (<b>E</b>) water purification filter wall structure made from silica sand permeable and filter bricks; (<b>F</b>) structure of silica sand filter well.</p>
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<p>(<b>A</b>) SEM image of the surface layer of the permeable and filterable brick; and (<b>B</b>) schematic diagram of the structure of the permeable and filterable brick.</p>
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<p>XPS spectra of the permeable surface of the water-permeable filter brick for Si2p (<b>A</b>) and C1s (<b>B</b>). The observed different colors refer to different elements or its chemical states for the easily distinguish and identify, as indicated by the arrow.</p>
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<p>(<b>A</b>) Schematic diagram of the water permeation mechanism of the permeable and filterable brick, (<b>B</b>) variation of water flux (<span class="html-italic">J</span>), porosity (<span class="html-italic">ε</span>), pore diameter (<span class="html-italic">r<sub>p</sub></span>), and membrane resistance (<span class="html-italic">R</span>) along the direction of water flow in the permeable and filterable brick.</p>
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<p>(<b>A</b>) The underwater oil contact angle of the water-permeable and filterable brick; (<b>B</b>) the oil-blocking effect of the water-permeable and filterable brick when wetted by water; (<b>C</b>) schematic diagram of the oil-blocking mechanism of the water-permeable and filterable brick when wetted by water.</p>
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<p>SEM observation of the biofilm on the surface of silicon sand filter bricks with different magnification. (<b>A</b>) ×5.00k; (<b>B</b>) ×20.0k; (<b>C</b>) ×5.00k; (<b>D</b>) ×30.0k.</p>
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<p>Schematic diagram of the biofilm in the silicon sand filter well: (<b>A</b>) Schematic diagram of denitrification mechanism, (<b>B</b>) Variation of the concentrations of COD, ammonia nitrogen, and nitrate nitrogen in each layer.</p>
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15 pages, 1837 KiB  
Article
Mitigation of Membrane Fouling in Membrane Bioreactors Using Granular and Powdered Activated Carbon: An Experimental Study
by Nataly Morales, Camila Mery-Araya, Paula Guerra, Rodrigo Poblete and Jaime Chacana-Olivares
Water 2024, 16(17), 2556; https://doi.org/10.3390/w16172556 - 9 Sep 2024
Viewed by 794
Abstract
This experimental study explores the mitigation of membrane fouling in membrane bioreactors (MBRs) through the combined use of granular activated carbon (GAC) and powdered activated carbon (PAC). The research assesses the impact of these materials on the fouling resistance, critical flux, and permeate [...] Read more.
This experimental study explores the mitigation of membrane fouling in membrane bioreactors (MBRs) through the combined use of granular activated carbon (GAC) and powdered activated carbon (PAC). The research assesses the impact of these materials on the fouling resistance, critical flux, and permeate quality using various mixed liquor suspended solids concentrations and carbon dosages. The results indicate that the GAC-PAC combination significantly reduces the total filtration resistance, particularly the cake layer resistance, by 11.7% to 13.6% compared to setups without activated carbon or with the individual carbon types. The study also reveals that this combination decreased the fouling rate by 15% to 24% at critical flux steps, demonstrating substantial improvements in fouling mitigation and operational efficiency. Furthermore, the GAC-PAC combination, which produces an adsorption process, enhances the permeate quality, achieving the near-complete removal of organic matter, total nitrogen, and turbidity, with total phosphorus removal reaching 99%. These findings demonstrate that the combined use of GAC and PAC not only reduces membrane fouling but also improves the overall MBR performance, making it a viable strategy for enhancing the efficiency of wastewater treatment processes. Full article
(This article belongs to the Special Issue Membrane Technology for Desalination and Wastewater Treatment)
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<p>Schematic of the experimental setup.</p>
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<p>Evolution of TMP during F<sub>c</sub> measurement of MBRs with GAC and PAC at various doses and combinations in MBR M1 and MBR M2.</p>
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<p>The evolution of the fouling rate during F<sub>c</sub> measurement for MBR M1 and MBR M2.</p>
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<p>Permeability for the tests conducted in MBR M1 and MBR M2.</p>
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<p>Initial increase in TMP (ΔP<sub>0</sub>) in MBR M1 and MBR M2.</p>
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<p>Intrinsic membrane resistance, total resistance, and cake layer resistance for MBR M1 and MBR M2.</p>
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14 pages, 3006 KiB  
Article
Manganese Oxide Enhanced Gravity-Driven Membrane (GDM) Filtration in Treating Iron- and Manganese-Containing Surface Water
by Jiaoying Luo, Yaru Zhang, Hailin Chang, Chenghai Lin, Yating Hu, Haochun Wang, Yanrui Wang and Xiaobin Tang
Water 2024, 16(17), 2374; https://doi.org/10.3390/w16172374 - 23 Aug 2024
Viewed by 594
Abstract
Manganese pollution in surface water has been a new concern in decentralized drinking water treatment. The dissolved manganese cannot be effectively removed by the traditional ultrafiltration (UF) process, but will cause severe membrane fouling. To address such issues, an innovative gravity-driven membrane (GDM) [...] Read more.
Manganese pollution in surface water has been a new concern in decentralized drinking water treatment. The dissolved manganese cannot be effectively removed by the traditional ultrafiltration (UF) process, but will cause severe membrane fouling. To address such issues, an innovative gravity-driven membrane (GDM) coupled with a dynamic manganese oxide (MnOx) film on the membrane surface was proposed, with hopes of enhancing manganese removal and alleviating membrane fouling. The results demonstrated that pre-coating a dynamic MnOx film on the membrane surface of a GDM system would effectively reduce start-up time for removing iron and manganese pollutants, without affecting the flux stabilization of the GDM. Effective manganese removal (~80%) primarily depended on the adsorption and auto-catalytic oxidation facilitated by the pre-coating of MnOx. Furthermore, the MnOx film notably enhanced organic pollutant removal efficiency. Additionally, the MnOx coated on the membrane surface acted as a skeleton, promoting the gradual formation of a biocake layer with a heterogeneous and porous structure, which benefited the flux stabilization of the GDM. In particular, the fine and homogeneous MnOx-M derived from the backflushing water of the mature manganese sand filter exhibited precise and uniform coating on the membrane surface, effectively mitigating the irreversible pore plugging caused by organic matter penetration and thereby enhancing stable flux by ~16.3% compared to the control. This study offered a novel strategy to enhance the purification efficiency of GDM system treating manganese pollution and was expected to contribute to the technological advancement of decentralized water supply scenarios. Full article
(This article belongs to the Special Issue Application of Membrane-Based Technology in Water Treatment)
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<p>Schematic diagram of the experimental GDM system.</p>
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<p>(<b>a</b>) Fe<sup>2+</sup> content in the feed water and GDM effluent; (<b>b</b>) averaged Fe<sup>2+</sup> removal efficiency.</p>
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<p>(<b>a</b>) Mn<sup>2+</sup> content in the feed water and GDM effluent; averaged Mn<sup>2+</sup> removal efficiency over (<b>b</b>) 2–12 days and (<b>c</b>) 34–39 days.</p>
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<p>(<b>a</b>,<b>c</b>) DOC and UV<sub>254</sub> content in the feed water and GDM effluent; (<b>b</b>,<b>d</b>) removal of DOC and UV<sub>254</sub> with GDM systems.</p>
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<p>Flux variation in the whole experiment (<b>a</b>) and five groups’ stable flux (<b>b</b>).</p>
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<p>The surface morphologies of the biocake layer in the GDM control, GDM + CMS, GDM + FMS, GDM + MnOx-S, and GDM + MnOx-M.</p>
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<p>The internal structure and stereo imaging morphology of the biocake layer in the GDM control, GDM + CMS, GDM + FMS, GDM + MnOx-S, and GDM + MnOx-M.</p>
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18 pages, 607 KiB  
Review
Sustainable Management and Advanced Nutrient Recovery from Biogas Energy Sector Effluents
by Magdalena Zielińska and Katarzyna Bułkowska
Energies 2024, 17(15), 3705; https://doi.org/10.3390/en17153705 - 27 Jul 2024
Viewed by 872
Abstract
Anaerobic digestion (AD) is an effective technology for the sustainable management of organic agricultural waste, producing both biogas and nutrient-rich digestate. This study aims to review and evaluate different methods for obtaining valuable products from digestate, with a focus on innovative and sustainable [...] Read more.
Anaerobic digestion (AD) is an effective technology for the sustainable management of organic agricultural waste, producing both biogas and nutrient-rich digestate. This study aims to review and evaluate different methods for obtaining valuable products from digestate, with a focus on innovative and sustainable approaches. The main objectives are to identify effective technologies for the recovery of nutrients and organic matter, assess their environmental and economic impact and outline the challenges and prospects in this area. The review covers established techniques (with a technology readiness level (TRL) of six to nine, indicating their maturity from pilot to full scale) such as struvite precipitation and ammonia stripping, which are very effective in recovering nitrogen and phosphorus from digestate and converting it into valuable biofertilizers. Struvite, for example, offers an option for slow-release fertilizers that reduces dependence on synthetic fertilizers. A comparative analysis shows that ammonia stripping can efficiently capture nitrogen and produce fertilizer without harming the environment. New methods, such as microalgae cultivation, use digestate as a nutrient source for the production of biofuels and bioplastics, contributing to renewable energy and sustainable material production. The study also examines composting and vermicomposting, where digestate is converted into nutrient-rich soil conditioners that significantly improve soil health and fertility. The production of biochar through pyrolysis is highlighted for its benefits in improving soil properties and sequestering carbon, providing a dual benefit for waste management and climate change mitigation. Membrane technologies, including ultrafiltration (UF) and reverse osmosis (RO), are being investigated for their effectiveness in nutrient recovery, despite challenges such as membrane fouling and high operating costs. The study highlights the potential of these valorization processes to improve the sustainability and economic viability of AD systems and to align with circular economy principles. The results suggest that the continuous optimization of these technologies and the integration of recycling processes are crucial to overcome existing challenges and realize their full potential. Full article
(This article belongs to the Section B: Energy and Environment)
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<p>Strategies for recovering valuable products from digestate.</p>
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19 pages, 2913 KiB  
Article
Long-Term Performance Evaluation and Fouling Characterization of a Full-Scale Brackish Water Reverse Osmosis Desalination Plant
by Sabrine Chebil, A. Ruiz-García, Soumaya Farhat and Mahmoud Bali
Water 2024, 16(13), 1892; https://doi.org/10.3390/w16131892 - 1 Jul 2024
Viewed by 926
Abstract
Water scarcity in Tunisia’s semi-arid regions necessitates advanced brackish water desalination solutions. This study evaluates the long-term performance and fouling characteristics of the largest brackish water reverse osmosis desalination plant in southern Tunisia over a period of 5026 days. The plant employs two-stage [...] Read more.
Water scarcity in Tunisia’s semi-arid regions necessitates advanced brackish water desalination solutions. This study evaluates the long-term performance and fouling characteristics of the largest brackish water reverse osmosis desalination plant in southern Tunisia over a period of 5026 days. The plant employs two-stage spiral-wound membrane elements to treat groundwater with a salinity of 3.2 g L−1. The pre-treatment process includes oxidation, sand filtration, and cartridge filtration, along with polyphosphonate antiscalant dosing. Membrane performance was assessed through the analysis of operational data, standardization of permeate flow (Qps) and salt passage (SPs), and the calculation of water (A), solute (B), and ionic (Bj) permeability coefficients. Over the operational period, there was an increase in operating pressure, pressure drop, and permeate conductivity, accompanied by a gradual increase in SPs as well as in the solute B and ionic Bj permeability coefficients. The average B increased by 82%, reflecting a decrease in solute rejection over time. Additionally, the ionic permeability coefficients for both SO42− and Cl ions increased, with Cl showing an 88% increase and SO42− showing an 87% increase. The produced water’s salinity increased by 67%, indicating a significant loss of membrane performance. To identify the cause of these problems, membrane characterization was analyzed using visual inspection, X-ray fluorescence (XRF), and Fourier transform infrared spectroscopy (FTIR). The characterization revealed the complex nature of the foulants, with a predominant presence of calcium sulfate, along with minor quantities of calcite, dolomite, and silica. The extent of CaSO4 deposition suggests poor antiscaling efficiency, highlighting the critical importance of selecting an effective antiscalant to mitigate membrane fouling. Full article
(This article belongs to the Topic Membrane Separation Technology Research)
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<p>BWRO desalination plant.</p>
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<p>Process diagram of the BWRO desalination plant.</p>
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<p>Reverse osmosis membrane cut out for autopsy tests.</p>
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<p>Evolution of operating data over time. (<b>a</b>) Feed pressure over time; (<b>b</b>) Pressure drop over time; (<b>c</b>) Conversion rate over time; (<b>d</b>) Permeate flow over time; (<b>e</b>) Permeate conductivity over time; (<b>f</b>) Specific energy consumption.</p>
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<p>Standardization of operating data. (<b>a</b>) Standardization of permeate flow; (<b>b</b>) Standardization of salt passage.</p>
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<p>Evolution of permeability coefficients. (<b>a</b>) Water permeability coefficient; (<b>b</b>) Solute permeability coefficient; (<b>c</b>) Sulfate ion permeability coefficient; (<b>d)</b> Chloride ion permeability coefficient.</p>
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<p>Fouling characterization. (<b>a</b>) Visual inspection of membrane fouling; (<b>b</b>) X-ray diffraction spectra of deposit sample; (<b>c</b>) IR spectra of deposit sample.</p>
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13 pages, 6793 KiB  
Article
Surface Reconstruction of Silicone-Based Amphiphilic Polymers for Mitigating Marine Biofouling
by Chuanying Wei, Yan Zhang, Zhen Tang, Changan Zhang, Jianhua Wu and Bo Wu
Polymers 2024, 16(11), 1570; https://doi.org/10.3390/polym16111570 - 1 Jun 2024
Viewed by 801
Abstract
Poly(dimethylsiloxane) (PDMS) coatings are considered to be environmentally friendly antifouling coatings. However, the presence of hydrophobic surfaces can enhance the adhesion rate of proteins, bacteria and microalgae, posing a challenge for biofouling removal. In this study, hydrophilic polymer chains were synthesised from methyl [...] Read more.
Poly(dimethylsiloxane) (PDMS) coatings are considered to be environmentally friendly antifouling coatings. However, the presence of hydrophobic surfaces can enhance the adhesion rate of proteins, bacteria and microalgae, posing a challenge for biofouling removal. In this study, hydrophilic polymer chains were synthesised from methyl methacrylate (MMA), Poly(ethylene glycol) methyl ether methacrylate (PEG-MA) and 3-(trimethoxysilyl) propyl methacrylate (TPMA). The crosslinking reaction between TPMA and PDMS results in the formation of a silicone-based amphiphilic co-network with surface reconstruction properties. The hydrophilic and hydrophobic domains are covalently bonded by condensation reactions, while the hydrophilic polymers migrate under water to induce surface reconstruction and form hydrogen bonds with water molecules to form a dense hydrated layer. This design effectively mitigates the adhesion of proteins, bacteria, algae and other marine organisms to the coating. The antifouling performance of the coatings was evaluated by assessing their adhesion rates to proteins (BSA-FITC), bacteria (B. subtilis and P. ruthenica) and algae (P. tricornutum). The results show that the amphiphilic co-network coating (e.g., P-AM-15) exhibits excellent antifouling properties against protein, bacterial and microalgal fouling. Furthermore, an overall assessment of its antifouling performance and stability was conducted in the East China Sea from 16 May to 12 September 2023, which showed that this silicon-based amphiphilic co-network coating remained intact with almost no marine organisms adhering to it. This study provides a novel approach for the development of high-performance silicone-based antifouling coatings. Full article
(This article belongs to the Section Polymer Applications)
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<p>(<b>a</b>) FT-IR spectra of the random copolymer poly(MMA-co-PEG-MA-co-TPMA). (<b>b</b>) ATR-IR spectra of PDMS and amphiphilic coatings with different additives. (<b>c</b>) SEM images of the coating, PDMS (<b>c1</b>), P-AM-5 (<b>c2</b>), P-AM-10 (<b>c3</b>) and P-AM-15 (<b>c4</b>). (<b>d</b>) The surface morphology images of the coating before and after immersion for 3 days.</p>
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<p>(<b>a</b>) Water and diiodomethane (CH<sub>2</sub>I<sub>2</sub>) contact angle tests of PDMS and P-AM-x coatings; the error bar represents the standard error derived from five independent replicates. (<b>b</b>) Surface free energy of PDMS and P-AM-x coatings. (<b>c</b>) The dynamic change process of water droplets and (<b>d</b>) the water dynamic contact angle of the coatings.</p>
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<p>(<b>a</b>) Adhesion rate of FITC-BSA. Coverage and anti-adhesion rate of <span class="html-italic">P. ruthenica</span> (<b>b</b>), <span class="html-italic">B. subtilis</span> (<b>c</b>) and <span class="html-italic">P.tricornutum</span> (<b>d</b>).</p>
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<p>Figures of panels coated with the PDMS coating and the P-AM-X coating immersed in Xiamen (24°56′ N, 118°10′ E) for 0 days and 4 months.</p>
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<p>Antifouling mechanisms of P-AM coatings against fouled organisms.</p>
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<p>(<b>a</b>) Synthesis of poly(MMA-co-PEG-MA-co-TPMA). (<b>b</b>) The synthesis route of the silicone-based amphiphilic co-networks coating. (<b>c</b>) Synthetic scheme.</p>
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13 pages, 4271 KiB  
Article
Comparison of Coagulation-Integrated Sand Filtration and Ultrafiltration for Seawater Reverse Osmosis Pretreatment
by Qingao Li, Lixin Xie, Shichang Xu and Wen Zhang
Membranes 2024, 14(6), 125; https://doi.org/10.3390/membranes14060125 - 29 May 2024
Viewed by 896
Abstract
The removal of dissolved organic matter (DOM) from seawater before the reverse osmosis (RO) processes is crucial for alleviating organic fouling of RO membranes. However, research is still insufficiently developed in the comparison of the effectiveness of integrating coagulation with ultrafiltration (UF) or [...] Read more.
The removal of dissolved organic matter (DOM) from seawater before the reverse osmosis (RO) processes is crucial for alleviating organic fouling of RO membranes. However, research is still insufficiently developed in the comparison of the effectiveness of integrating coagulation with ultrafiltration (UF) or sand filtration (SF) in the pretreatment stage of seawater reverse osmosis (SWRO) for the removal of DOM. In this study, we investigated the effect of pretreatment technologies on RO fouling caused by DOM in seawater, including the integration of coagulation and sand filtration (C-S pretreatment) and the integration of coagulation and ultrafiltration (C-U pretreatment). Both integrated pretreatments achieved comparable DOM removal rates (70.2% for C-U and 69.6% for C-S), and C-S exhibited enhanced removal of UV-absorbing compounds. Although C-U was more proficient in reducing the silt density index (below 2) compared to C-S (above 3) and improved the elimination of humic acid-like organics, it left a higher proportion of tyrosine-protein-like organics, soluble microbial by-product-like organics, and finer organics in the effluent, leading to the formation of a dense cake layer on RO membrane and a higher flux decline. Therefore, suitable technologies should be selected according to specific water conditions to efficiently mitigate RO membrane fouling. Full article
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<p>Schematic diagram of integrated seawater pretreatment processes.</p>
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<p>Removal ratio of turbidity, UV<sub>254</sub> and DOC of different coagulants in the coagulation treatment of the raw seawater. (<b>a</b>) PAC, (<b>b</b>) FeCl<sub>3</sub>.</p>
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<p>EEM spectra and FRI analysis of organics in effluent before or after coagulation. (<b>a</b>) Raw water, (<b>b</b>) PAC at a concentration of 5 mg·L<sup>−1</sup>, (<b>c</b>) PAC at a concentration of 30 mg·L<sup>−1</sup>, (<b>d</b>) FeCl<sub>3</sub> at a concentration of 5 mg·L<sup>−1</sup>, (<b>e</b>) FeCl<sub>3</sub> at a concentration of 10 mg·L<sup>−1</sup>, (<b>f</b>) fluorescence intensity of effluent after being pretreated by PAC or FeCl<sub>3</sub> (Regions I, II, III, IV, and V were noted in the EEM spectras, corresponding to tyrosine protein-like organics, tryptophan protein-like organics, fulvic acid-like organics, soluble microbial by-product-like (SMP-like) organics, and humic acid-like organics, respectively).</p>
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<p>The content of hydrophilic, transphilic and hydrophobic fractions of organics in raw water and water treated with 30 mg·L<sup>−1</sup> PAC and 10 mg·L<sup>−1</sup> FeCl<sub>3</sub>.</p>
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<p>Removal ratio of UV<sub>254</sub>, DOC, and turbidity in the coagulation (10 mg·L<sup>−1</sup> FeCl<sub>3</sub>), C-S and C-U pretreatments.</p>
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<p>EEM spectra and FRI analysis of organics in effluent after treatment with (<b>a</b>) C-S or (<b>b</b>) C-U pretreatment; (<b>c</b>) fluorescence intensity of effluent after treatment with C-S or C-U pretreatment (Regions I, II, III, IV, and V were noted in the EEM spectras, corresponding to tyrosine protein-like organics, tryptophan protein-like organics, fulvic acid-like organics, soluble microbial by-product-like (SMP-like) organics, and humic acid-like organics, respectively).</p>
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<p>The content of hydrophilic, transphilic and hydrophobic fractions of organics in the effluent pretreated with coagulation (10 mg·L<sup>−1</sup> FeCl<sub>3</sub>), C-S or C-U pretreatment.</p>
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<p>Effect of integrated pretreatments on normalized RO membrane flux.</p>
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<p>SEM images and their corresponding EDX mapping images. (<b>a</b>) Virgin RO membrane, (<b>b</b>) fouled RO membrane after C-S pretreatment, and (<b>c</b>) fouled RO membrane after C-U pretreatment.</p>
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141 KiB  
Abstract
Application of Electrochemical Processes to Membrane Bioreactors for Sustainable Wastewater Treatment: A Short Review
by Fabiano Castrogiovanni
Proceedings 2024, 105(1), 46; https://doi.org/10.3390/proceedings2024105046 - 28 May 2024
Viewed by 202
Abstract
Membrane bioreactors (MBRs) are considered as innovative systems for wastewater treatment in line with sustainable development and the reuse of treated wastewater. One of the main problems of MBRs is the fouling of the membrane modules, defined as fouling, which affects both the [...] Read more.
Membrane bioreactors (MBRs) are considered as innovative systems for wastewater treatment in line with sustainable development and the reuse of treated wastewater. One of the main problems of MBRs is the fouling of the membrane modules, defined as fouling, which affects both the stability and the effectiveness of the biological purification process. Among the many technologies developed by the scientific community for the mitigation of fouling, the application of electrochemical processes to MBRs has attracted considerable interest. It has been observed that these processes present greater simplicity from a management point of view and, at the same time, allow an improvement in the purification performance of the system, achieving greater purification efficiencies compared to conventional MBR systems. Unlike traditional chemical and physical cleaning methods, which cause a reduction in the useful life of the membranes and require higher operating costs, these systems, defined as membrane electrobioreactors (eMBRs), can prove economically advantageous. This technology does not involve the addition of chemical substances in the reactor, which can alter the characteristics of the wastewater. It is also simple from a management point of view and can be easily monitored in situ. The eMBR configurations used must be evaluated on the basis of different operating conditions, as a correct balance of parameters is essential for achieving the set objectives. This paper seeks to review technologies proposed for wastewater treatment using eMBRs. Finally, the challenges in applying these removal strategies are also highlighted in this brief review. Full article
14 pages, 4833 KiB  
Article
Environmentally Friendly and Efficient Methods for Mitigating the Density of Ascidian Fouling in Mediterranean Mussel Farming
by Dimitrios Tsotsios, Dimitrios K. Papadopoulos, Maria V. Alvanou, Ioannis Georgoulis, Athanasios Lattos, Basile Michaelidis, Konstantinos Feidantsis, Ioannis A. Giantsis and John A. Theodorou
Fishes 2024, 9(4), 135; https://doi.org/10.3390/fishes9040135 - 14 Apr 2024
Cited by 3 | Viewed by 1053
Abstract
Ascidian biofouling generates significant challenges to bivalve aquaculture. Their rapid spread across almost every available surface leads to increased maintenance costs and reduced yields in shellfish farming. In addition, ascidians may introduce pathogens or toxins, further compromising the health and marketability of bivalve [...] Read more.
Ascidian biofouling generates significant challenges to bivalve aquaculture. Their rapid spread across almost every available surface leads to increased maintenance costs and reduced yields in shellfish farming. In addition, ascidians may introduce pathogens or toxins, further compromising the health and marketability of bivalve stocks and thereby necessitating strict management strategies to manage these impacts. The aim of this study was the evaluation of different management practices for eliminating ascidian fouling and the identification of the best method for Mytilus galloprovincialis (Lamarck, 1819) aquaculture farms. The effects of different anti-fouling treatments as well as their interactive outcomes were examined by conducting two experiments. Various experimental procedures were applied, including the temporally differential washing of mussels, air exposure and immersion in 50 ppt and 70 ppt salinity solutions, as well as the combination of these applications. All treatments reduced the number of ascidian colonies on mussel socks but at varying proportions. Immersing mussel socks in a 70 ppt salinity solution followed by air exposure for 1 day was the most efficient method and led to a 93% eradication. Full article
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Figure 1

Figure 1
<p>Map location of the Amvrakikos Gulf and the area of Mazoma Lagoon where the mussel farm in which the field experimental procedure was conducted is located. Coordinates: 39.025628318910435, 20.7571601812546.</p>
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<p>Longline and raft mussel farm installation located close to the Mazoma Lagoon (northwest coast of Amvrakikos Gulf) (<b>A</b>); where mussel socks were placed (<b>B</b>). Mussel socks before (<b>C</b>) and after (<b>D</b>) the washing with sea water and/or air exposure; (<b>C</b>,<b>D</b>) were obtained after transferring the mussels to a sunny place in order for them to be better displayed.</p>
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<p>Schematic representation of experiment 1 in the four different groups of mussel socks (a–d), as described in the <a href="#sec2dot3-fishes-09-00135" class="html-sec">Section 2.3</a>.</p>
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<p>Schematic representation of the experimental protocol employing sea water tanks of different salinities and different immersion times of mussels.</p>
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<p>Schematic representation of experiment 2.</p>
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<p>Seasonal variations in sea water temperature, oxygen and Chl-α concentration in the Mazoma Lagoon mussel farm.</p>
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<p>Fifteen-day washing effect for a period of 5 months on the number of ascidian colonies of the mussel socks. Values are mean ± S.D. of <span class="html-italic">n</span> = 4. Lower case letters denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between different time periods of intervention, while asterisks (*) denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between control and treated mussels.</p>
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<p>Thirty-day washing (<b>A</b>), air exposure (<b>B</b>), combination of washing and air exposure effect (<b>C</b>) and comparison between all treatments (<b>D</b>) for a period of five months on the number of ascidian colonies of the mussel socks. Values are mean ± S.D. of <span class="html-italic">n</span> = 4. Lower case letters denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between different time periods of intervention, asterisks (*) denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between control and treated mussel socks, and carets (^) denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between different treatments.</p>
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<p>Effect of immersion in 50 and 70 ppt sea water for 3 and 5 min and exposure to air on the number (<b>A</b>) and the (<b>B</b>) % maintenance of ascidian colonies on the mussel socks. Values are mean ± S.D. of <span class="html-italic">n</span> = 4. Asterisks (*) denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) between control and treated mussel socks and carets (^) denote statistically significant differences (<span class="html-italic">p</span> &lt; 0.05) before and after treatment (<b>A</b>) and between different time exposures (3 and 5 min) (<b>B</b>).</p>
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