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17 pages, 5358 KiB  
Article
A PDA@ZIF-8-Incorporated PMIA TFN-FO Membrane for Seawater Desalination: Improving Water Flux and Anti-Fouling Performance
by Yu Ma, Rui Jia, Zhen-Liang Xu, Aida Aibulatova, Xiao-Gang Jin, Yin-Xin Fang, Ming-Xiao Zhang and Sun-Jie Xu
Membranes 2024, 14(12), 272; https://doi.org/10.3390/membranes14120272 (registering DOI) - 16 Dec 2024
Abstract
Forward osmosis (FO) technology, known for its minimal energy requirements, excellent resistance to fouling, and significant commercial potential, shows enormous promise in the development of sustainable technologies, especially with regard to seawater desalination and wastewater. In this study, we improved the performance of [...] Read more.
Forward osmosis (FO) technology, known for its minimal energy requirements, excellent resistance to fouling, and significant commercial potential, shows enormous promise in the development of sustainable technologies, especially with regard to seawater desalination and wastewater. In this study, we improved the performance of the FO membrane in terms of its mechanical strength and hydrophilic properties. Generally, the water flux (Jw) of polyisophenylbenzamide (PMIA) thin-film composite (TFC)-FO membranes is still inadequate for industrial applications. Here, hydrophilic polydopamine (PDA)@ zeolitic imidazolate frameworks-8 (ZIF-8) nanomaterials and their integration into PMIA membranes using the interfacial polymerization (IP) method were investigated. The impact of PDA@ZIF-8 on membrane performance in both pressure-retarded osmosis (PRO) and forward osmosis (FO) modes was analyzed. The durability and fouling resistance of these membranes were evaluated over the long term. When the amount of ZIF-8@PDA incorporated in the membrane reached 0.05 wt% in the aqueous phase in the IP reaction, the Jw values for the PRO mode and FO mode were 12.09 LMH and 11.10 LMH, respectively. The reverse salt flux (Js)/Jw values for both modes decreased from 0.75 and 0.80 to 0.33 and 0.35, respectively. At the same time, the PRO and FO modes’ properties were stable in a 15 h test. The incorporation of PDA@ZIF-8 facilitated the formation of water channels within the nanoparticle pores. Furthermore, the Js/Jw ratio decreased significantly, and the FO membranes containing PDA@ZIF-8 exhibited high flux recovery rates and superior resistance to membrane fouling. Therefore, PDA@ZIF-8-modified FO membranes have the potential for use in industrial applications in seawater desalination. Full article
(This article belongs to the Section Membrane Applications for Water Treatment)
34 pages, 1759 KiB  
Review
Promoting a Circular Economy in Mining Practices
by Subin Antony Jose, Joy Calhoun, Otoniel B. Renteria, Pedro Mercado, Shinichiro Nakajima, Colton N. Hope, Mario Sotelo and Pradeep L. Menezes
Sustainability 2024, 16(24), 11016; https://doi.org/10.3390/su162411016 - 16 Dec 2024
Viewed by 116
Abstract
Integrating circular economy (CE) principles into mining practices offers a promising path toward reducing environmental harm while promoting sustainable resource management. This shift boosts the industry’s efficiency and profitability and aligns it with global sustainability goals. This paper delves into strategies for closing [...] Read more.
Integrating circular economy (CE) principles into mining practices offers a promising path toward reducing environmental harm while promoting sustainable resource management. This shift boosts the industry’s efficiency and profitability and aligns it with global sustainability goals. This paper delves into strategies for closing material loops, such as waste valorization, resource recovery from mine tailings, and water reuse in mining processes. Additionally, this study highlights innovative technologies and their potential to transform traditional linear practices into sustainable, circular systems. This paper emphasizes the importance of strong collaboration among industry stakeholders and policymakers, including mining companies, researchers, and local communities, for the implementation of CE principles. This paper also discusses the role of emerging digital tools, automation, and artificial intelligence in advancing circular practices and improving operational efficiency. By exploring the economic, environmental, and social benefits of the CE, this paper demonstrates how these practices can contribute to sustainable mining. It addresses key challenges, including technological, economic, and regulatory hurdles, and offers recommendations for overcoming them to pave the way for a more sustainable and resilient mining industry. Full article
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Figure 1
<p>A typical mineral/metal ore process (the blue boxes are wet processes [<a href="#B30-sustainability-16-11016" class="html-bibr">30</a>]).</p>
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<p>Optimization of the material life cycle through CE principles, modified to show a larger emphasis on exploitation as it relates to mining (reproduced with permission from [<a href="#B78-sustainability-16-11016" class="html-bibr">78</a>]).</p>
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<p>Inputs and outputs of mine water, including traditional and non-traditional sources, with beneficial or loss outcomes.</p>
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<p>Overview of how CE in sustainable mining integrates closure and rehabilitation planning from exploration to actual site closure. Adapted from [<a href="#B110-sustainability-16-11016" class="html-bibr">110</a>].</p>
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<p>Worldwide electronic waste generation per capita in 2019 (in kilograms per person) (reproduced with permission from [<a href="#B130-sustainability-16-11016" class="html-bibr">130</a>]).</p>
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<p>Major research and development challenges in circular economy categories. Adapted from [<a href="#B145-sustainability-16-11016" class="html-bibr">145</a>].</p>
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15 pages, 5476 KiB  
Article
ZnO–Polyaniline Nanocomposite Functionalised with Laccase Enzymes for Electrochemical Detection of Cetyltrimethylammonuium Bromide (CTAB)
by Hilda Dinah Kyomuhimbo, Usisipho Feleni, Nils Hendrik Haneklaus and Hendrik Gideon Brink
J. Xenobiot. 2024, 14(4), 1988-2002; https://doi.org/10.3390/jox14040106 (registering DOI) - 16 Dec 2024
Viewed by 206
Abstract
The direct discharge of cationic surfactants into environmental matrices has exponentially increased due to their wide application in many products. These compounds and their degraded products disrupt microbial dynamics, hinder plant survival, and affect human health. Therefore, there is an urgent need to [...] Read more.
The direct discharge of cationic surfactants into environmental matrices has exponentially increased due to their wide application in many products. These compounds and their degraded products disrupt microbial dynamics, hinder plant survival, and affect human health. Therefore, there is an urgent need to develop electroanalytical assessment techniques for their identification, determination, and monitoring. In our study, ZnO-PANI nanocomposites were electrodeposited on a glassy carbon electrode (GCE), followed by the immobilization of laccase enzymes and the electrodeposition of polypyrrole (PPy), to form a biosensor that was used for the detection of CTAB. A UV-Vis analysis showed bands corresponding to the π-π* transition of benzenoid and quinoid rings, π-polaron band transition and n-π*polaronic transitions associated with the extended coil chain conformation of PANI, and the presence and interaction of ZnO with PANI and type 3 copper in the laccase enzymes. The FTIR analysis exhibited peaks corresponding to N-H and C-N stretches and bends for amine, C=C stretches for conjugated alkenes, and a C-H bend for aromatic compounds. A high-resolution scanning electron microscopy (HRSEM) analysis proved that PANI and ZnO-PANI were deposited as fibres with hairy topography resulting from covalent bonding with the laccase enzymes. The modified electrode (PPy-6/GCE) was used as a platform for the detection of CTAB with three linear ranges of 0.5–100 µM, 200–500 µM, and 700–1900 µM. The sensor displayed a high sensitivity of 0.935 μA μM−1 cm−2, a detection limit of 0.0116 µM, and acceptable recoveries of 95.02% and 87.84% for tap water and wastewater, respectively. Full article
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Graphical abstract

Graphical abstract
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<p>A graph of (<b>A</b>) UV-Vis analysis and (<b>B</b>) Tauc plots for PANI and ZnO-PANI and PPy-Lac-ZnO-PANI composites.</p>
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<p>FTIR spectra for (<b>A</b>) PANI and (<b>B</b>) ZnO-PANI and (<b>C</b>) PPy-Lac-ZnO-PANI composites.</p>
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<p>SEM and EDS for (<b>A</b>,<b>B</b>) blank SPCE and (<b>C</b>,<b>D</b>) PANI-, (<b>E</b>,<b>F</b>) ZnO-PANI-, and (<b>G</b>,<b>H</b>) PPy-Lac-ZnO-PANI-modified SPCEs.</p>
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<p>Graphs showing electrochemical deposition of (<b>A</b>) PANI, (<b>B</b>) ZnO-PANI, and (<b>C</b>) PPy; (<b>D</b>,<b>E</b>) effect of ZnO loading on the conductivity of PANI; CV of (<b>F</b>) PANI and (<b>G</b>) ZnO-PANI at varying scan rates; and (<b>H</b>) Randles–Ševčík plot for PANI and ZnO-PANI composites.</p>
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<p>Cyclic voltammograms of different electrodes in the (<b>A</b>) absence and (<b>B</b>) presence of 20 µM CTAB in 0.1 M PBS. (<b>C</b>) A graph of electrode activity (peak current) at varying pH of the solution. (<b>D</b>) Effect of pH on conductivity of electrode and peak current vs. concentration of CTAB in 0.1 M PBS. (<b>E</b>) DPV of CTAB at different concentrations in PBS.</p>
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<p>(<b>A</b>) Cyclic voltammogram of PPy-Lac-ZnO-PANI/GCE electrode in 0.01 M ABTS in 0.1 M PBS and (<b>B</b>) Randles–Ševčík plot for PPy-Lac-ZnO-PANI/GCE in 0.01 M ABTS in 0.1 M PBS.</p>
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<p>Performance of the PPy/Lac-ZnO-PANI/GCE in presence of (<b>A</b>) interferants and (<b>B</b>) in real water samples and reusability of the biosensor in (<b>C</b>) PBS and (<b>D</b>) in tap water and wastewater.</p>
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<p>Performance of the PPy/Lac-ZnO-PANI/GCE in presence of (<b>A</b>) interferants and (<b>B</b>) in real water samples and reusability of the biosensor in (<b>C</b>) PBS and (<b>D</b>) in tap water and wastewater.</p>
Full article ">Scheme 1
<p>Suggested mechanism for electrochemical oxidation of CTAB [<a href="#B70-jox-14-00106" class="html-bibr">70</a>,<a href="#B71-jox-14-00106" class="html-bibr">71</a>].</p>
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13 pages, 4035 KiB  
Communication
Use of Laccase Enzymes as Bio-Receptors for the Organic Dye Methylene Blue in a Surface Plasmon Resonance Biosensor
by Araceli Sánchez-Álvarez, Gabriela Elizabeth Quintanilla-Villanueva, Osvaldo Rodríguez-Quiroz, Melissa Marlene Rodríguez-Delgado, Juan Francisco Villarreal-Chiu, Analía Sicardi-Segade and Donato Luna-Moreno
Sensors 2024, 24(24), 8008; https://doi.org/10.3390/s24248008 (registering DOI) - 15 Dec 2024
Viewed by 304
Abstract
Methylene blue is a cationic organic dye commonly found in wastewater, groundwater, and surface water due to industrial discharge into the environment. This emerging pollutant is notably persistent and can pose risks to both human health and the environment. In this study, we [...] Read more.
Methylene blue is a cationic organic dye commonly found in wastewater, groundwater, and surface water due to industrial discharge into the environment. This emerging pollutant is notably persistent and can pose risks to both human health and the environment. In this study, we developed a Surface Plasmon Resonance Biosensor employing a BK7 prism coated with 3 nm chromium and 50 nm of gold in the Kretschmann configuration, specifically for the detection of methylene blue. For the first time, laccases immobilized on a gold surface were utilized as bio-receptors for this organic dye. The enzyme was immobilized using carbodiimide bonds with EDC/NHS crosslinkers, allowing for the analysis of samples with minimal preparation. The method demonstrated validation with a limit of detection (LOD) of 4.61 mg L−1 and a limit of quantification (LOQ) of 15.37 mg L−1, a working range of 0–100 mg L−1, and an R2 value of 0.9614 during real-time analysis. A rainwater sample spiked with methylene blue yielded a recovery rate of 122.46 ± 4.41%. The biosensor maintained a stable signal over 17 cycles and remained effective for 30 days at room temperature. Full article
(This article belongs to the Section Biosensors)
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Figure 1

Figure 1
<p>Chemical structure of methylene blue.</p>
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<p>Possible recognition process and first step of degradation of methylene blue by laccases.</p>
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<p>Immobilization process of laccases on the thin chromium–gold film chip. In the step 1, alkanethiols are added to the thin gold surface. In step 2, the EDC is added, forming an unstable intermediate. In step 3, the NHS is added, creating a sulfo-NHS ester. In step 4, NHS is replaced by the laccase through an amide bond.</p>
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<p>Assembly of the prism and the chip on the SPR equipment: (<b>a</b>) assembly of the prism, the chip with a thin gold film with the immobilized laccases, the prism and other components. (<b>b</b>) Set up of the prism, sample cell, chip with immobilized laccases and the other on the SPR equipment.</p>
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<p>Reflectance spectra obtained by angular sweep.</p>
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<p>Immobilization process of laccass from <span class="html-italic">Rhus vernicifera</span> in real-time by SPR.</p>
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<p>FTIR analysis of different stages of laccase immobilization.</p>
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<p>(<b>a</b>) SPR analysis of stocks with different concentrations of methylene blue. (<b>b</b>) Calibration curve and equation of a straight line.</p>
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<p>Comparison of the intensity of reflectance of solutions of methylene blue at day 1 and day 30.</p>
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16 pages, 10766 KiB  
Article
Investigating the Impact of Polymers on Clay Flocculation and Residual Oil Behaviour Using a 2.5D Model
by Xianda Sun, Yuchen Wang, Qiansong Guo, Zhaozhuo Ouyang, Chengwu Xu, Yangdong Cao, Tao Liu and Wenjun Ma
Polymers 2024, 16(24), 3494; https://doi.org/10.3390/polym16243494 - 14 Dec 2024
Viewed by 284
Abstract
In the process of oilfield development, the surfactant–polymer (SP) composite system has shown significant effects in enhancing oil recovery (EOR) due to its excellent interfacial activity and viscoelastic properties. However, with the continuous increase in the volume of composite flooding injection, a decline [...] Read more.
In the process of oilfield development, the surfactant–polymer (SP) composite system has shown significant effects in enhancing oil recovery (EOR) due to its excellent interfacial activity and viscoelastic properties. However, with the continuous increase in the volume of composite flooding injection, a decline in injection–production capacity (I/P capacity) has been observed. Through the observation of frozen core slices, it was found that during the secondary composite flooding (SCF) process, a large amount of residual oil in the form of intergranular adsorption remained in the core pores. This phenomenon suggests that the displacement efficiency of the composite flooding may be affected. Research has shown that polymers undergo flocculation reactions with clay minerals (such as kaolinite, Kln) in the reservoir, leading to the formation of high-viscosity mixtures of migrating particles and crude oil (CO). These high-viscosity mixtures accumulate in local pores, making it difficult to further displace them, which causes oil trapping and negatively affects the overall displacement efficiency of secondary composite flooding (SCF). To explore this mechanism, this study used a microscopic visualization displacement model (MVDM) and microscopy techniques to observe the migration of particles during secondary composite flooding. By using kaolinite water suspension (Kln-WS) to simulate migrating particles in the reservoir, the displacement effects of the composite flooding system on the kaolinite water suspension, crude oil, and their mixtures were observed. Experimental results showed that the polymer, acting as a flocculant, promoted the flocculation of kaolinite during the displacement process, thereby increasing the viscosity of crude oil and affecting the displacement efficiency of secondary composite flooding. Full article
(This article belongs to the Section Polymer Applications)
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Figure 1

Figure 1
<p>Inter-particle adsorption of residual oil diagram.</p>
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<p>Inter-particle adsorption of residual oil in (<b>a</b>) CT 3D image and (<b>b</b>) fluorescence photograph.</p>
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<p>Flocculation diagram. (<b>a</b>) Kaolinite water suspension. (<b>b</b>) Formation of flocs. (<b>c</b>) Precipitation.</p>
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<p>Experimental apparatus diagram. 1 Micro-injection pump. 2 Injection syringe. 3 Microscope. 4 Valve. 5 Micro-visualization model holder. 6 Micro-visualization model. 7 Heating plate. 8 Parallel light source. 9 Liquid recovery collection container. 10 Image acquisition computer.</p>
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<p>Cast thin sheet. (<b>a</b>) Laser confocal scanning injection thin sheet; (<b>b</b>) vectorized image after vectorization by software(Imagine v1.7.1).</p>
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<p>Microscopic displacement etching model.</p>
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<p>Kaolinite aqueous suspension (30% concentration), transmitted light photograph, temperature 46 °C.</p>
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<p>The oil displacement effect images from Experiment 1 are as follows. (<b>a</b>) Waterflooding (10 PV) transmitted light photograph. (<b>b</b>) Binary composite flooding (10 PV) transmitted light photograph. (<b>c</b>) Waterflooding (20 PV) transmitted light photograph. (<b>d</b>) Binary composite flooding (20 PV) transmitted light photograph.</p>
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<p>The oil displacement effect images from Experiment 2 are as follows. (<b>a</b>) Binary composite flooding (10 PV) displacement effect. (<b>b</b>) Binary composite flooding (20 PV) displacement effect. (<b>c</b>) Binary composite flooding (80 PV) displacement effect.</p>
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<p>The oil displacement effect images from Experiment 3 are as follows. (<b>a</b>) Binary composite flooding (10 PV) displacement effect. (<b>b</b>) Binary composite flooding (20 PV) displacement effect. (<b>c</b>) Binary composite flooding (80 PV) displacement effect.</p>
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<p>The distribution of the mixed solution is shown as follows: (<b>a</b>) transmitted light photograph and (<b>b</b>) orthogonal light photograph.</p>
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<p>The schematic of residual oil distribution types is as follows. 1 Pore surface film-type. 2 Grain adsorption-type. 3 Corner-type. 4 Throat-type. 5 Cluster-type. 6 Intergranular adsorption-type.</p>
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<p>The residual oil distribution types are as follows. (<b>a</b>) Cluster-type. (<b>b</b>) Throat-type. (<b>c</b>) Pore surface film-type. (<b>d</b>) Corner-type. (The arrow points to the location where the residual oil is located).</p>
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11 pages, 3351 KiB  
Article
Emulsive Liquid–Liquid Microextraction for the Determination of Phthalic Acid Esters in Environmental Water Samples
by Xinyuan Bi, Chi Zhang, Xiaorong Xue, Shangjun Su, Zhiping Yang, Xu Jing and Qiang Zhang
Molecules 2024, 29(24), 5908; https://doi.org/10.3390/molecules29245908 (registering DOI) - 14 Dec 2024
Viewed by 290
Abstract
A convenient, rapid, and environmentally friendly method, emulsive liquid–liquid microextraction combined with high-performance liquid chromatography, was established to determine phthalic acid esters in tap, river, lake, and sea water. After the method’s optimization, we obtained the appropriate volume of the extractant and pure [...] Read more.
A convenient, rapid, and environmentally friendly method, emulsive liquid–liquid microextraction combined with high-performance liquid chromatography, was established to determine phthalic acid esters in tap, river, lake, and sea water. After the method’s optimization, we obtained the appropriate volume of the extractant and pure water, the number of strokes, the separation methods, the mass volume fraction of the demulsifier, the demulsifier volume, the sample volume, the salt amount, and the pH conditions. This method requires only 200 μL of heptanoic acid (fatty acid) as the extractant and 75 mg of sodium acetate as demulsifiers for fast microextraction and separation, respectively, avoiding the use of further equipment. Emulsive liquid–liquid microextraction offers substantial advantages over dispersive liquid–liquid microextraction by eliminating the need for toxic dispersants, thereby preventing any influences of dispersants on the partition coefficients. The linear range of detection ranged from 0.5 to 50 μg L−1, with a limit of detection of 0.2 μg L−1 and a limit of quantitation of 0.5 μg L−1. The recoveries ranged from 80.2% to 106.3%, and the relative standard deviations ranged between 0.5% and 6.7%. Five greenness metrics confirmed that this method is environmentally friendly and aligns with the principles of green analytical chemistry. The proposed method achieved a greenness score of 8.42, surpassing that of other methods as evaluated using the SPMS. The novel method may well be a valuable technique for determining phthalic acid esters in water samples. Full article
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Figure 1
<p>Optimization of ELLME parameters: (<b>A</b>) extractant volume; (<b>B</b>) pure water volume; (<b>C</b>) number of strokes; (<b>D</b>) separation method; (<b>E</b>) demulsifier mass volume fraction (% <span class="html-italic">w</span>/<span class="html-italic">v</span>); (<b>F</b>) demulsifier volume; (<b>G</b>) sample volume; (<b>H</b>) sodium acetate amount; (<b>I</b>) pH (the error bar represents the standard deviation).</p>
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<p>The flowchart of the ELLME-HPLC-UV/Vis by Figdraw 2.0 software.</p>
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27 pages, 22816 KiB  
Article
Aqueous Carbonation of Waste Incineration Residues: Comparing BA, FA, and APCr Across Production Scenarios
by Quentin Wehrung, Davide Bernasconi, Enrico Destefanis, Caterina Caviglia, Nadia Curetti, Sara Di Felice, Erica Bicchi, Alessandro Pavese and Linda Pastero
Minerals 2024, 14(12), 1269; https://doi.org/10.3390/min14121269 - 13 Dec 2024
Viewed by 348
Abstract
This study investigates the reactivity of municipal solid waste incineration residues to aqueous carbonation, focusing on CO2 absorption rates, uptakes, and heavy metal (HM) leachability. Various combinations of boiler, electrofilter, and bag filter residues were assessed under typical incineration conditions. Bag filter [...] Read more.
This study investigates the reactivity of municipal solid waste incineration residues to aqueous carbonation, focusing on CO2 absorption rates, uptakes, and heavy metal (HM) leachability. Various combinations of boiler, electrofilter, and bag filter residues were assessed under typical incineration conditions. Bag filter residues from lime-sorbent plants exhibited the highest CO2 uptake (244.5 gCO2/kg), while bottom ash (BA) fine fraction, boiler/electrofilter fly ash (FA), and other mixed air pollution control residue (APCr) demonstrated uptakes of 101, 0, 93, and 167 gCO2/kg, respectively. Carbonation kinetics revealed that high calcium content FA and APCr, followed similar CO2 absorption trends. Notably, BA carbonation was predominantly driven by Ca-aluminates rather than lime. Carbonation reduces leaching of Al, As, Cd, Co, Cu, Ni, Pb and Zn compared to water washing, though significant concerns arise with anions such as Sb and Cr. In BA, critical behaviours of Cr, Mn, and Fe were observed, with Cr leaching likely controlled by Fe-Mn-Cr oxide particle dissolution. These findings highlight the potential of integrating enhanced metal recovery (EMR) through density or magnetic separation in BA prior to carbonation to reduce HM leaching and recycle critical metals (Ag, Cu, Cr, Ni, Mn, etc). Full article
(This article belongs to the Special Issue CO2 Mineralization and Utilization)
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Figure 1

Figure 1
<p>MSWI process diagram of a typical electricity and heat cogeneration plant, showing the collection points of the solid residues: BA, FA, APCr as well as the most common solid additives (lignite powder, lime, sodium bicarbonate). Not to scale. Note that electrofilter residues can be classified as either FA or APCr, depending on whether additives were used upstream.</p>
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<p>Methodology for selecting representative samples to assess carbonation reactivity across common MSWI residue production scenarios, highlighting the five raw selected samples for this study: (<b>A</b>): BA under 0.25 mm, (<b>B</b>): FA from boiler and electrofilter, (<b>C</b>): APCr from boiler and electrofilter, (<b>D</b>): APCr from boiler, electrofilter and bag filter, (<b>E</b>): APCr from bag filter.</p>
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<p>XRPD patterns for (<b>A</b>) sample A (<b>B</b>) sample B (<b>C</b>) sample C (<b>D</b>) sample D (<b>E</b>) sample E. Legend for the XRPD mineral phases: C: Corundum (standard), Z: ZnO (standard) 1: CaClOH, 2: portlandite, 3: magnesite, 4: calcite, 5: anhydrite, 6: halite, 7: sylvite, 8: hatrurite, 9: larnite, 10: sinjarite, 11: CaCl<sub>2</sub>·4H<sub>2</sub>O, 12: periclase, 13: melilite, 14: lime, 15: quartz, 16: cristobalite, 17: hydrocalumite, 18: hannebachite, 19: ilmenite/perovskite, 20: merwinite, 21: bassanite, 22: singenite, 23: K-tetrachlorozincate, 24: gehlenite, 25: katoite, 26: hydroxiapatite, akermanite: 27, mullite: 28.</p>
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<p>SEM-EDS patterns of characteristic phases and minerals observed in sample A. (<b>A</b>–<b>C</b>) illustrate a zoom-in from the sample's bulk matrix to a Ca-Al particle exhibiting a botryoidal morphology.</p>
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<p>SEM-EDS patterns of characteristic phases and minerals observed in sample B. (<b>A</b>–<b>C</b>) illustrate a zoom-in from the sample’s bulk matrix to the surface of a glass sphere.</p>
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<p>SEM-EDS patterns of characteristic phases and minerals observed in sample C.</p>
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<p>SEM-EDS patterns of characteristic phases and minerals observed in sample D. (<b>A</b>–<b>C</b>,<b>G</b>–<b>I</b>) illustrate a zoom-in from the sample’s bulk matrix to typical particle aggregates. (<b>C</b>,<b>E</b>,<b>F</b>,<b>I</b>) show aggregates with well-grown trigonal calcite crystals. Characteristic CaClOH sheared morphology is visible in (<b>I</b>). (<b>D</b>) depicts the compact CCHO structure, with its surface free of nanoparticle adsorption.</p>
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<p>SEM-EDS patterns of characteristic phases and minerals observed in sample E. (<b>A</b>–<b>C</b>) illustrate a zoom-in from the sample's bulk matrix to a typical aggregate composed of heterogeneous, CaClOH-rich nanoparticles, along with a NaCl microcrystal. (<b>D</b>) shows slag particles rich in Mg, S, K, Ca, Cl, Fe, and Al, along with NaCl microcrystals. (<b>E</b>) displays a typical aggregate with characteristic CaClOH sheared morphology. (<b>F</b>) depictss a Ca-silicate, likely larnite.</p>
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<p>Stoichiometric carbonation capacity (gCO<sub>2</sub>/kg) reported for 1 kg of FA/APCr, based on free CaO, Ca(OH)<sub>2</sub>, CaCl<sub>2</sub>·2H<sub>2</sub>O, Ca<sub>2</sub>SiO<sub>4</sub>, Ca<sub>3</sub>SiO<sub>5</sub>, MgO, Mg(OH)<sub>2</sub>, Ca<sub>2</sub>Al(OH)<sub>6</sub>Cl·2H<sub>2</sub>O, Ca<sub>3</sub>Al<sub>2</sub>(OH)<sub>12</sub> and Ca<sub>12</sub>Al<sub>14</sub>O<sub>33</sub> content, as calculated according to the equations listed in <a href="#minerals-14-01269-t004" class="html-table">Table 4</a>.</p>
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<p>Comparison of CO<sub>2</sub> absorption rate patterns as a function of time for the samples studied (exp. identifiers: A1, B1, C1, D1, E1).</p>
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<p>XRPD patterns for (<b>A</b>) sample A (<b>B</b>) sample B (<b>C</b>) sample C (<b>D</b>) sample D (<b>E</b>) sample E. Legend for the XRPD mineral phases: 2: Portlandite, 4: Calcite, 5: Anhydrite, 6: Halite, 9: Larnite, 10: Sinjarite, 12: Periclase, 15: Quartz, 17: Hydrocalumite, 18: Hannebachite, 20: Merwinite, 25: Katoite, 28: Mullite. The nomenclature used in the XRPD legend of <a href="#minerals-14-01269-f003" class="html-fig">Figure 3</a> was maintained for consistency.</p>
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<p>HM concentrations from TCLP on raw samples, carbonated samples, and wastewater from aqueous carbonation and water-washing experiments for (<b>A</b>) sample A (<b>B</b>) sample B (<b>C</b>) sample C (<b>D</b>) sample D (<b>E</b>) sample E. Note the logarithmic scale. Note that the washing wastewater correspond to an L/S of 40, while the TCLP leachates have an L/S of 10.</p>
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<p>Backscattered electron SEM images of hydrocalumite in a raw sample A polished section. Colours identify elements, recognised by SEM-EDX mapping: magenta, Ca; blue, Al; green, Cl.</p>
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<p>Backscattered electron SEM images of a Cr-Mn-Fe oxide with Ca-aluminate coating in a raw sample A polished section. Right image: Colors identify phases, recognized by SEM-EDS mapping: blue, Fe oxide; cyan, Cr-Mn-Fe oxide; yellow, Mn oxide; red, Mn-Fe oxide; magenta, Ca-aluminate.</p>
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<p>Proposed mechanism of chromium leaching during BA carbonation due to Ca-aluminate coating breakdown and Cr-Mn-Fe oxides decomposition. Both trivalent (Cr<sup>3+</sup>) and hexavalent (CrO<sub>4</sub><sup>2–</sup>) chromium were represented.</p>
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12 pages, 2871 KiB  
Article
Recovery of Cellulose Contained in Mixed Fabrics
by Juan A. Conesa and Viviana N. Córdoba
Processes 2024, 12(12), 2854; https://doi.org/10.3390/pr12122854 - 12 Dec 2024
Viewed by 338
Abstract
The present work focuses on the recovery of cellulose from mixed fabrics containing polyester and cotton through the use of different chemical and hydrothermal treatment methods. Through the application of various analytical techniques, such as thermogravimetry (TG) and infrared spectroscopy (IR), we seek [...] Read more.
The present work focuses on the recovery of cellulose from mixed fabrics containing polyester and cotton through the use of different chemical and hydrothermal treatment methods. Through the application of various analytical techniques, such as thermogravimetry (TG) and infrared spectroscopy (IR), we seek to determine the effectiveness of the methods used. The results indicate that different treatments with NaOH and distilled water at high temperatures and pressures are particularly effective for the extraction of the cellulose fraction. Furthermore, these methods were compared with previous studies to evaluate their feasibility and sustainability. The findings underline the importance of selecting appropriate experimental conditions to maximize the purity of the cellulose obtained and minimize fiber degradation, thus promoting more efficient and sustainable textile recycling processes. These results have significant implications for industrial applications by enabling the development of scalable recycling methods and contribute to reducing the environmental impact of textile waste. Full article
(This article belongs to the Special Issue Novel Recovery Technologies from Wastewater and Waste)
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<p>Thermogravimetry (TG) curves of (<b>a</b>) samples treated with different combinations of hydroxides and urea, (<b>b</b>) samples treated with PEG/NaOH under different temperature and time conditions, (<b>c</b>) samples treated with different concentrations of NaOH at high temperature (225 °C), (<b>d</b>) samples treated with different concentrations of HCl.</p>
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<p>Micrographs of cellulose fibers. (<b>a</b>) Sample M0 untreated fabric, (<b>b</b>) sample MR1 treated with 0.1 g NaOH at 225 °C.</p>
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<p>Micrographs of cellulose fibers. (<b>a</b>) Sample M0 untreated fabric, (<b>b</b>) sample MR6 treated with HCl 0.025 g at 225 °C.</p>
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<p>IR spectra of the untreated (M0) and treated tissues most prominently under different experimental conditions (M1, M2 and M5).</p>
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<p>IR spectra of untreated tissue (M0) and tissue treated with NaOH at different concentrations (MR1, MR2 and MR3).</p>
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<p>IR spectra of untreated tissue (M0) and tissue treated with HCl and H<sub>2</sub>O under different experimental conditions (MR6, MR7 and MR8).</p>
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16 pages, 2198 KiB  
Article
Decontamination and Circular Economy of Dredged Material and Mining Waters Using Adiabatic Sonic Evaporation and Crystallization (ASEC) Technology
by T. Ángel DelValls, Julián Blasco, Sebastián Vera, Nuria O. Núñez and Estefanía Bonnail
Appl. Sci. 2024, 14(24), 11593; https://doi.org/10.3390/app142411593 - 12 Dec 2024
Viewed by 391
Abstract
Dredged material is a common environmental and economic issue worldwide. Tons of highly contaminated material, derived from cleaning the bottoms of bays and harbours, are stored until depuration. These volumes occupy huge extensions and require costly treatments. The Ria of Huelva (southwest Spain) [...] Read more.
Dredged material is a common environmental and economic issue worldwide. Tons of highly contaminated material, derived from cleaning the bottoms of bays and harbours, are stored until depuration. These volumes occupy huge extensions and require costly treatments. The Ria of Huelva (southwest Spain) receives additionally high metal contamination inputs from the Odiel and Tinto Rivers which are strongly affected by acid mine drainage (acid lixiviates with high metal content and sulphates). These two circumstances convert the port of Huelva into an acceptor/accumulator of contamination. The current study proposes an alternative active treatment of dredged material and mining residues using ASEC (Adiabatic Sonic Evaporation and Crystallization) technology to obtain distilled water and valuable solid conglomerates. Different samples were depurated and the efficiency of the technology was tested. The results show a complete recovery of the treated volumes with high-quality water (pH~7, EC < 56 µS/cm, complete removal of dissolved elements). Also, the characterization of the dried solids enable the calculation of approximate revenues from the valorization of some potentially exploitable elements (Rio Tinto: 4 M, Tharsis: 3.7 M, dredged material: 2.5 M USD/yr). The avoidance of residue discharge plus the aggregated value would promote a circular economy in sectors such as mining and dredging activities. Full article
(This article belongs to the Section Environmental Sciences)
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<p>Odiel-Rio Tinto River watershed in the province of Huelva (southwest Spain), the main affected courses according to [<a href="#B35-applsci-14-11593" class="html-bibr">35</a>], and the location of the sampling points (Tharsis mine, Puente Gadea/Rio Tinto River and the Port of Huelva-supplier dredged material).</p>
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<p>Collected samples (<b>top left</b>) and the treated fluid (<b>top right</b>) from the Rio Tinto river, Tharsis mine and the dredged material. Below are the results in crystallized solids after the treatment with ASEC technology.</p>
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<p>Elemental composition (in %) of the crystallized solid samples from Rio Tinto (<b>a</b>), Tharsis (<b>b</b>) and dredged material (<b>c</b>) after ASEC depuration.</p>
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<p>X-ray difraction results of the crystallized solids from Rio Tinto (<b>a</b>), Tharsis (<b>b</b>) and dredged material (<b>c</b>). Correspondence between coloured peaks and composition found in samples.</p>
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22 pages, 4372 KiB  
Article
Impact of CO2 Viscosity and Capillary Pressure on Water Production in Homogeneous and Heterogeneous Media
by Ali Zidane
Water 2024, 16(24), 3566; https://doi.org/10.3390/w16243566 - 11 Dec 2024
Viewed by 301
Abstract
This study explores the numerical modeling of CO2 injection in water within a lab-scale domain, where the dimensions are in the order of centimeters, highlighting its diverse applications and significant environmental and economic benefits. The investigation focuses on the impacts of heterogeneity, [...] Read more.
This study explores the numerical modeling of CO2 injection in water within a lab-scale domain, where the dimensions are in the order of centimeters, highlighting its diverse applications and significant environmental and economic benefits. The investigation focuses on the impacts of heterogeneity, capillary pressure, and CO2 viscosification on water production. Findings reveal that increasing CO2 viscosity by a factor of 5 drastically influences water production, while further increasing it to a factor of 10 yields minimal additional effect. Capillary pressure notably delays breakthrough and reduces sweeping efficiency (effectiveness of the injected CO2 in displacing water), with a more pronounced impact in slim cores (1 cm) compared to thick cores (3.8 cm). The numerical modeling of CO2 injection in water within a lab-scale domain provides valuable insights into enhanced oil recovery (EOR) techniques. These optimized strategies can improve the efficiency and effectiveness of CO2-EOR, leading to increased oil and gas recovery from reservoirs. Full article
(This article belongs to the Special Issue Hydraulic Engineering and Numerical Simulation of Two-Phase Flows)
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<p>Simulation domain and discretization grids: Example 1.</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water production for different viscosification cases.</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water production for different viscosification cases.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water production with and without capillary pressure.</p>
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<p>Heterogeneous core with two permeability layers.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water production with and without capillary pressure.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water saturation at 10% PVI; with (<b>a</b>) and without (<b>b</b>) capillary pressure. Water saturation at 20% PVI; with (<b>c</b>) and without (<b>d</b>) capillary pressure. Water saturation at 30% PVI; with (<b>e</b>) and without (<b>f</b>) capillary pressure.</p>
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<p>Water production with and without capillary pressure.</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water saturation at 10% PVI; base case (<b>a</b>), 5× viscosification (<b>b</b>) and 10× viscosification (<b>c</b>). Water saturation at 20% PVI; base case (<b>d</b>), 5× viscosification (<b>e</b>) and 10× viscosification (<b>f</b>). Water saturation at 30% PVI; base case (<b>g</b>), 5× viscosification (<b>h</b>) and 10× viscosification (<b>i</b>).</p>
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<p>Water production with different viscosification levels.</p>
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<p>Verification of the numerical model with analytical solution.</p>
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19 pages, 2651 KiB  
Article
Cationic/Anionic Poly(p-Phenylene Oxide) Membranes: Preparation and Electrodialysis Performance for Nickel Recovery from Industrial Effluents
by Fabrício Wilbert, Joana Farias Corte, Felipe Tiago do Nascimento, Vanusca Dalosto Jahno, Marco Antônio Siqueira Rodrigues, Fabrício Celso, Salatiel W. da Silva and Andrea Moura Bernardes
Membranes 2024, 14(12), 268; https://doi.org/10.3390/membranes14120268 - 11 Dec 2024
Viewed by 401
Abstract
Electrodialysis (ED) has already been applied to recover nickel in galvanizing processes, allowing nickel recovery and the production of a treated effluent with demineralized water quality. However, the growth in ED use is still limited by the production and commercialization of ion-selective membranes, [...] Read more.
Electrodialysis (ED) has already been applied to recover nickel in galvanizing processes, allowing nickel recovery and the production of a treated effluent with demineralized water quality. However, the growth in ED use is still limited by the production and commercialization of ion-selective membranes, currently limited to a few large companies. Therefore, this paper presents the development of homogeneous cationic and anionic membranes made from poly(2,6-dimethyl-1,4-phenylene oxide) (PPO) for ED use. Cationic membranes were prepared by the sulfonation reaction of PPO under different experimental conditions (PPO:H2SO4 molar ratio and reaction time). Anionic membranes were prepared by the bromination reaction of PPO, followed by the amination reaction. The membranes were characterized for their chemical and electrochemical properties, including ion exchange capacity, conductivity, thermal stability, and surface morphology. The optimal conditions for cationic membrane sulfonation were achieved with a 1:4.4 PPO:H2SO4 molar ratio, and a reaction time of 0.5 h. For anionic membranes, the best results were obtained with bromination, with a PPO:NBS (N-Bromosuccinimide) molar ratio of 1:0.5, followed by 14 days of amination. Overall, 91.8% chloride, 90.9% sulfate, and 85.5% nickel ion extraction was achieved, highlighting PPO as a promising polymer for the development of anionic and cationic ion-selective membranes for ED. Full article
(This article belongs to the Special Issue Research on Electrodialytic Processes)
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<p>Electrodialysis bench system used for nickel wastewater treatment.</p>
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<p>SEM surface images of the cationic membranes HDX 100 and CATPPO-1.</p>
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<p>SEM surface images of the anionic membranes HDX200 and ANIPPO-1.</p>
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<p>Current–voltage curves of CATPPO-1 membrane in sodium sulfate solution (<b>a</b>) or nickel industrial effluent (<b>b</b>) and of HDX100 membrane in sodium sulfate solution (<b>c</b>) or nickel industrial effluent (<b>d</b>).</p>
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<p>Current–voltage curves of CATPPO-1 membrane in sodium sulfate solution (<b>a</b>) or nickel industrial effluent (<b>b</b>) and of HDX100 membrane in sodium sulfate solution (<b>c</b>) or nickel industrial effluent (<b>d</b>).</p>
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<p>Current–voltage curves of ANIPPO-1 membrane in sodium sulfate solution (<b>a</b>) or nickel industrial effluent (<b>b</b>) and of HDX200 membrane in sodium sulfate solution (<b>c</b>) or nickel industrial effluent (<b>d</b>).</p>
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<p>Current–voltage curves of ANIPPO-1 membrane in sodium sulfate solution (<b>a</b>) or nickel industrial effluent (<b>b</b>) and of HDX200 membrane in sodium sulfate solution (<b>c</b>) or nickel industrial effluent (<b>d</b>).</p>
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29 pages, 7779 KiB  
Article
Removal of Iron(II) as Magnetite from Acid Mine Water
by Mokgadi Gladness Rapeta, Johannes Philippus Maree and Titus Makudali Msagati
Minerals 2024, 14(12), 1256; https://doi.org/10.3390/min14121256 - 10 Dec 2024
Viewed by 336
Abstract
The High-Density Sludge (HDS) process is widely used for the treatment of acid mine water as it produces a sludge of high density. The aim of this study was the development of a process where iron in mine water can be removed as [...] Read more.
The High-Density Sludge (HDS) process is widely used for the treatment of acid mine water as it produces a sludge of high density. The aim of this study was the development of a process where iron in mine water can be removed as magnetite, to assist with rapid settling of sludge. It was concluded that Fe2+ can be removed as Fe3O4 (magnetite) by forming Fe(OH)2 and Fe(OH)3 in the mole ratio of 1:2. Magnetite can form in the absence or presence of gypsum. The settling rate of magnetite-rich sludge is substantially faster than that of ferric hydroxide-rich sludge. It is recommended that further studies be carried out on the separation of magnetite gypsum through magnetic separation. Full article
(This article belongs to the Section Environmental Mineralogy and Biogeochemistry)
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<p>Neutralisation process of High-Density Sludge for AMD treatment [<a href="#B3-minerals-14-01256" class="html-bibr">3</a>,<a href="#B12-minerals-14-01256" class="html-bibr">12</a>].</p>
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<p>Effect of pH on Fe(OH)<sub>2</sub> precipitation (OLI simulation).</p>
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<p>Magnetite produced with NaOH as alkali.</p>
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<p>SEM-EDS image of Fe<sub>3</sub>O<sub>4</sub> at pH 11 dried at 25 (<b>top</b>) and 100℃ (<b>bottom</b>).</p>
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<p>SEM-EDS image of Fe<sub>3</sub>O<sub>4</sub> at pH 11 dried at 25 (<b>top</b>) and 100℃ (<b>bottom</b>).</p>
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<p>Particle size of Fe<sub>3</sub>O<sub>4</sub> (pH 11) measured using Zetasizer.</p>
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<p>Goethite formation from Fe(OH)<sub>3</sub> when only CaCO<sub>3</sub> was used for treatment.</p>
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<p>SEM/EDS images of goethite (<b>top</b>) and hematite (<b>bottom</b>).</p>
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<p>XRD spectra of goethite.</p>
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<p>XRD spectra of hematite.</p>
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<p>SEM/EDS images of Fe<sub>3</sub>O<sub>4</sub>–CaSO<sub>4</sub> for instant (<b>top</b>) and multiple (<b>bottom</b>) dosing.</p>
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<p>XRD spectra for Fe<sub>3</sub>O<sub>4</sub>-CaSO<sub>4</sub> in instant dosing.</p>
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<p>XRD spectra for Fe<sub>3</sub>O<sub>4</sub>–CaSO<sub>4</sub> in multiple dosing.</p>
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<p>Particle size of Fe<sub>3</sub>O<sub>4</sub>–CaSO<sub>4</sub> (instant and multiple dosing) measured using Zetasizer.</p>
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<p>Particle size of Fe<sub>3</sub>O<sub>4</sub>–CaSO<sub>4</sub> (instant and multiple dosing) measured using Zetasizer.</p>
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<p>Settling of Fe(OH)<sub>3</sub> and Fe<sub>3</sub>O<sub>4</sub>-rich sludge.</p>
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<p>Sludge settling for (<b>i</b>) Fe(OH)<sub>3</sub>-rich sludge and (<b>ii</b>) Fe<sub>3</sub>O<sub>4</sub>-rich sludge.</p>
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15 pages, 2142 KiB  
Article
Growth and C:N:P Stoichiometry of Pinus yunnanensis Seedlings in Response to Drought and Rewatering
by Chengyao Liu, Junwen Wu, Jianyao Gu and Huaijiao Duan
Forests 2024, 15(12), 2175; https://doi.org/10.3390/f15122175 - 10 Dec 2024
Viewed by 414
Abstract
Pinus yunnanensis has high economic and ecological value. The survival of P. yunnanensis has been greatly affected by global warming. This study examines the response of P. yunnanensis seedlings to drought stress and their recovery following rewatering, focusing on growth metrics and C:N:P [...] Read more.
Pinus yunnanensis has high economic and ecological value. The survival of P. yunnanensis has been greatly affected by global warming. This study examines the response of P. yunnanensis seedlings to drought stress and their recovery following rewatering, focusing on growth metrics and C:N:P stoichiometry. This experiment included the four following treatments: CK (water content was 90% ± 5%); LS (water content was 75% ± 5%); MS (water content was 60% ± 5%); and SS (water content was 45% ± 5%). This experiment also included a continuous drought period of 30 days followed by 7 days of rewatering. This study found that drought limited the growth of seedlings, and seedlings could recover rapidly from the damage caused by LS and MS treatments after rewatering, and the recovery of seedlings was greater following LS and MS treatments than following SS. After the drought, the C content in the leaves and stems of P. yunnanensis seedlings could recover to CK levels after rewatering. The N content of each organ and the P content of fine roots of P. yunnanensis seedlings showed an upward trend after rewatering. In summary, the growth of P. yunnanensis seedlings was significantly affected by drought stress, and the recovery mechanism of rewatering varied depending on the degree of drought. Combining the phenotypic plasticity index and principal component analysis, the stem biomass, thin root biomass, root/shoot ratio, leaf C:P, leaf N:P, leaf P, stem C:P, thin root N, thin root P, coarse root N, coarse root P, and coarse root C were the most important indexes for adaptation to drought and rewatering. Full article
(This article belongs to the Section Forest Ecophysiology and Biology)
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<p>Effects of drought and rewatering on the plant height and ground diameter growth of seedlings. Different lowercase letters on the columns indicate significant differences among drought treatments at the same stage (<span class="html-italic">p</span> &lt; 0.05). CK (water content was 90% ± 5%), LS (water content was 75% ± 5%), MS (water content was 60% ± 5%), and SS (water content was 45% ± 5%).</p>
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<p>Effect of drought and rewatering on the biomass of seedlings. Different lowercase letters on the figure columns indicate significant differences among drought treatments at the same stage (<span class="html-italic">p</span> &lt; 0.05). CK (water content was 90% ± 5%), LS (water content was 75% ± 5%), MS (water content was 60% ± 5%), and SS (water content was 45% ± 5%).</p>
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<p>Effect of drought and rewatering on the biomass proportions of seedlings. Different lowercase letters on the figure columns indicate significant differences among drought treatments at the same stage (<span class="html-italic">p</span> &lt; 0.05). CK (water content was 90% ± 5%), LS (water content was 75% ± 5%), MS (water content was 60% ± 5%), and SS (water content was 45% ± 5%).</p>
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<p>Changes in C, N, and P contents in seedlings after drought and rewatering. Different lowercase letters on the figure columns indicate significant differences among drought treatments at the same stage (<span class="html-italic">p</span> &lt; 0.05). CK (water content was 90% ± 5%), LS (water content was 75% ± 5%), MS (water content was 60% ± 5%), and SS (water content was 45% ± 5%).</p>
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<p>Changes in C:N, C:P, and N:P ratios of seedlings after drought and rewatering. Different lowercase letters on the figure columns indicate significant differences among drought treatments at the same stage (<span class="html-italic">p</span> &lt; 0.05). CK (water content was 90% ± 5%), LS (water content was 75% ± 5%), MS (water content was 60% ± 5%), and SS (water content was 45% ± 5%).</p>
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<p>The phenotypic plasticity index of seedlings after rewatering.</p>
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<p>Flowchart of drought and rewatering experiment of <span class="html-italic">P. yunnanensis</span> seedlings.</p>
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18 pages, 4414 KiB  
Article
Development of an Original Integrated System for Heat Recovery from Coolant in the Machining Process and Investigation of Its Efficiency
by Osman Şahin and Durmuş Karayel
Appl. Sci. 2024, 14(24), 11499; https://doi.org/10.3390/app142411499 - 10 Dec 2024
Viewed by 357
Abstract
When a comparison is made between production methods, it will be seen that a significant amount of energy is consumed in machining processes and a large part of this energy is lost as waste heat. This is an important risk factor for both [...] Read more.
When a comparison is made between production methods, it will be seen that a significant amount of energy is consumed in machining processes and a large part of this energy is lost as waste heat. This is an important risk factor for both energy efficiency and environmental protection. During metalworking, a very high level of heat is generated at the cutting tool–workpiece interface. We have conducted a comprehensive literature study on this subject, but so far, no study has been found on the recovery of the heat generated in machining processes. Therefore, the aim and motivation of this study is to recover this waste heat to a certain extent. For this purpose, a comprehensive coolant temperature control and heat recovery system has been developed. This system, which was produced as a prototype, can be easily integrated into the machine tool and automatically adjust the coolant temperature to a certain constant temperature level and maintain this temperature value throughout the process. More importantly, it recovers the heat energy taken from the coolant and makes it useful. On the other hand, although it is not the subject of this study, cutting performance increases, coolant consumption decreases and tool life is extended with the cooling of the coolant. Thus, environmental risks are also reduced. Also, the efficiency and economic feasibility of the developed system were also examined. For this purpose, the energy amount consumed by the developed system and the machine tool were measured separately, and the total energy consumed was determined. Then, the consumed and recovered energy amounts were compared, and it was seen that the amount of energy recovered was more than the total amount of energy consumed. When the decrease in coolant and cutting-tool consumption is also taken into account compared to the classical cooling system, it is understood that the amortization period of the developed system is quite low. On the other hand, optimum conditions were investigated in order to provide maximum energy recovery. For this purpose, experiments were carried out by drilling 2592 holes on 27 samples, 96 holes in each sample, by taking the coolant solution ratio, cutting speed, and feed rate as variable parameters. The experimental results were evaluated using the Taguchi method. It has been observed that the system can be easily adapted to other machining processes, such as turning and milling, and that it has a high potential to increase energy efficiency and prevent environmental risks in this area. Full article
(This article belongs to the Special Issue Treatment of Wastes and Energy Recovery)
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<p>Schematic diagram of the circuit elements of the developed heat recovery system.</p>
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<p>Photo of the developed cooling and recovery system.</p>
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<p>Datalogger used in the experiments.</p>
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<p>Machine tool used in experiments.</p>
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<p>The experimental setup.</p>
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<p>Dimensions of test specimen.</p>
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<p>G83 peck drilling cycle.</p>
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<p>Energy consumptions for 15 °C coolant temperature.</p>
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<p>Energy consumptions for 20 °C coolant temperature.</p>
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<p>Consumed total energy and recovered energy for 15 °C coolant temperatures.</p>
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<p>Energy recovery S/N analysis graph.</p>
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<p>Contour graphs when the heat recovery system is off (at room temperature).</p>
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<p>Consumed total energy and recovered energy for 20 °C coolant temperatures.</p>
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<p>Energy recovery S/N analysis graph.</p>
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<p>Contour graphs for room temperature.</p>
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15 pages, 4643 KiB  
Article
Comparing Recovery Volumes of Steady and Unsteady Injections into an Aquifer Storage and Recovery Well
by Saeid Masoudiashtiani and Richard C. Peralta
Earth 2024, 5(4), 990-1004; https://doi.org/10.3390/earth5040051 - 9 Dec 2024
Viewed by 562
Abstract
Aquifer Storage and Recovery (ASR) can involve injecting available surface water into an unconfined aquifer and then extracting it to provide secondary water for irrigation. This study demonstrates a method for evaluating the appropriateness of steady injection versus unsteady injection for an assumed [...] Read more.
Aquifer Storage and Recovery (ASR) can involve injecting available surface water into an unconfined aquifer and then extracting it to provide secondary water for irrigation. This study demonstrates a method for evaluating the appropriateness of steady injection versus unsteady injection for an assumed situation. In design, it can be important to affect the transient: the proportion of the injected water that would be subsequently extracted (versus that remaining in the aquifer) and the proportion within the extracted water that would be an injectate (versus ambient groundwater). These proportions can be predicted from the predicted value of an ASR well’s Recovery Effectiveness (REN)—the time-varying proportion of injectate that is extracted subsequently from the same fully penetrating well. Applying the demonstrated procedure with appropriately detailed data and simulation models can predict the REN values resulting from steady versus unsteady injection, followed by steady extraction. For convenience in displaying and computing REN, the injectate was assumed to have a 100 ppm conservative solute concentration. For this demonstration, a homogenous isotropic unconfined one-layer aquifer was assumed. The scenarios involved steady or unsteady injection for 61 days via a fully penetrating ASR well. Then, 91 days of steady pumping led to the extraction of a total volume equal to that injected. For the assumed hydrogeologic data—31 years of Salt Lake City, Utah, rainfall data and estimated captured runoff—the results show that steady injection is more likely to cause a predictable REN but might not cause a higher REN than daily varying injection of the same total volume. Assuming different runoff or hydrogeologic flows would lead to different REN values. Steady injection causes a predictable groundwater mound and can assure a sufficient vadose zone thickness for overlying plants. Augmentation and storage of captured rainwater can help to provide a steady injection rate. For a situation that requires REN management, appropriate simulations can help water managers design ASR systems that will achieve REN goals and increase sustainable groundwater availability. Full article
(This article belongs to the Topic Human Impact on Groundwater Environment)
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<p>Residential area (Site 5) and weather stations at the international airport and Triad Center in Salt Lake County, UT, USA.</p>
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<p>Modeled area for simulation of ASR well (top view) (not to scale).</p>
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<p>Modeled area for simulation of ASR well (side view) (not to scale).</p>
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<p>Total April–May runoff volumes of the 31 years in Site 5 simulated via WinSLAMM 10.4.1 software.</p>
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<p>REN (gm/gm) values of every half month during extraction for Demo 1; continuous (steady) extraction rate equals the injection volume divided by 91 days for every 31 years. Extraction volume equals the injection volume.</p>
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<p>REN (gm/gm) values of every half month during extraction for Demo 2; continuous (steady) extraction rate equals the injection volume divided by 91 days for every 31 years. Extraction volume equals the injection volume.</p>
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<p>USGS Observation Well no. 4044441115505501 (Hydrologic Unit no. 16020204), with a latitude of 40°44′45″, a longitude of 111°55′06″ NAD27, and a land surface altitude of 1283.2 m (4210 ft.) above NGVD29. The well is 15.0 ft. (4.57 m) below the land surface and located about 350 m (1148.29 ft.) away from the residential area (Site 5) in Salt Lake County, Utah, USA (URL: <a href="http://waterdata.usgs.gov/nwis/inventory?agency_code=USGS&amp;site_no=404444111550501" target="_blank">http://waterdata.usgs.gov/nwis/inventory?agency_code=USGS&amp;site_no=404444111550501</a>, accessed on 1 October 2007).</p>
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<p>Available observed groundwater levels from 1982 to 1990 reported by USGS Observation Well no. 404444111550501 located about 350 m (1148.29 ft.) away from Site 5. The depth to groundwater level in April and May for the years is between 1.1 (3.6) and 1.4 m (4.6 ft.).</p>
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<p>Simulated daily flows at the well resulting from 61 days of unsteady and steady injections (positive magnitudes), followed by 91 days of steady extraction (negative magnitudes), for an ASR well at Site 5 in 2001.</p>
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<p>Simulated groundwater levels at the well resulting from 61 days of unsteady and steady injections, followed by 91 days of steady extraction, for an ASR well at Site 5 in 2001 (Note: the elevation datum is equal to zero).</p>
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