Nothing Special   »   [go: up one dir, main page]

You seem to have javascript disabled. Please note that many of the page functionalities won't work as expected without javascript enabled.
 
 

Topic Editors

Department of Chemical Engineering, Toronto Metropolitan University (Formerly Ryerson University), 350 Victoria Street, Toronto, ON M5B 2K3, Canada
Department of Civil Engineering, Universidad de Cartagena, Sede Piedra de Bolívar, Avenida del Consulado 48-152, Cartagena, Colombia
School of Occupational and Public Health, Toronto Metropolitan University, 350 Victoria Street, Toronto, ON M5B 2K3, Canada
Dr. Samira Ghafoori
1. Department of Chemical Engineering, Faculty of Engineering & Architectural Science, Toronto Metropolitan University (Formelry Ryerson University), Toronto, ON, Canada
2. Sanofi in Canada, Toronto, ON, Canada

Wastewater Treatment by Physical, Chemical, Photochemical, and Biological Processes, and Their Combinations

Abstract submission deadline
closed (30 September 2024)
Manuscript submission deadline
31 December 2024
Viewed by
23681

Topic Information

Dear Colleagues,

Due to the limitations of individual physical, chemical, photochemical, or biological processes in their effectiveness or economic feasibility, most processes are not cost-effective or efficient on their own to treat wastewaters, such as high-strength wastewaters. Advanced oxidation processes (AOPs) are alternatives to treat wastewaters containing non-biodegradable, toxic, inhibitory, and recalcitrant organic contaminants. Although the main advantages of AOPs are their destructive and non-selective nature, as well as their high rates of reactions in comparison to biological processes, they may not be cost-effective on their own. An alternative treatment is the biodegradability enhancement of wastewater by a photochemical pre-treatment or post-treatment using AOPs. Therefore, the focus of this topic is on the latest developments in all AOPs, including photochemical reaction engineering, photoreactor design and kinetics, photocatalyst development, biological processes for wastewater treatment including high-strength actual wastewaters, biokinetics, technical improvements for municipal wastewater treatment plants including process control, and/or combinations of different physical, chemical, photochemical, and biological processes to maximize organic degradation in wastewater while being cost-effective.

Prof. Dr. Mehrab Mehrvar
Dr. Edgar Quiñones-Bolaños
Dr. Ciro Bustillo-Lecompte
Dr. Samira Ghafoori
Topic Editors

Keywords

  • photochemical reaction engineering
  • advanced oxidation technologies
  • biological wastewater treatment
  • biokinetics
  • combined AOPs with other processes including biological processes
  • high-strength wastewater treatment
  • actual wastewater treatment
  • optimization and modelling of combined processes for wastewater treatment
  • industrial wastewater treatment applications

Participating Journals

Journal Name Impact Factor CiteScore Launched Year First Decision (median) APC
Bioengineering
bioengineering
3.8 4.0 2014 15.6 Days CHF 2700 Submit
Catalysts
catalysts
3.8 6.8 2011 12.9 Days CHF 2200 Submit
Processes
processes
2.8 5.1 2013 14.4 Days CHF 2400 Submit
Sustainability
sustainability
3.3 6.8 2009 20 Days CHF 2400 Submit
Water
water
3.0 5.8 2009 16.5 Days CHF 2600 Submit

Preprints.org is a multidiscipline platform providing preprint service that is dedicated to sharing your research from the start and empowering your research journey.

MDPI Topics is cooperating with Preprints.org and has built a direct connection between MDPI journals and Preprints.org. Authors are encouraged to enjoy the benefits by posting a preprint at Preprints.org prior to publication:

  1. Immediately share your ideas ahead of publication and establish your research priority;
  2. Protect your idea from being stolen with this time-stamped preprint article;
  3. Enhance the exposure and impact of your research;
  4. Receive feedback from your peers in advance;
  5. Have it indexed in Web of Science (Preprint Citation Index), Google Scholar, Crossref, SHARE, PrePubMed, Scilit and Europe PMC.

Published Papers (15 papers)

Order results
Result details
Journals
Select all
Export citation of selected articles as:
18 pages, 2553 KiB  
Article
Performance Evaluation of Sponge Anaerobic Baffled Reactor for Municipal Wastewater Treatment
by Nadeem Ullah, Zeshan Sheikh, Owais Ahmad and Sher Jamal Khan
Sustainability 2024, 16(21), 9398; https://doi.org/10.3390/su16219398 - 29 Oct 2024
Viewed by 768
Abstract
The anaerobic baffled reactor (ABR) is a decentralized treatment system that is commonly used for municipal wastewater treatment. Slower growth rate of anaerobic microorganisms requires extended hydraulic retention time (HRT), leading to a larger bioreactor volume. In this study, polyurethane sponge sheets were [...] Read more.
The anaerobic baffled reactor (ABR) is a decentralized treatment system that is commonly used for municipal wastewater treatment. Slower growth rate of anaerobic microorganisms requires extended hydraulic retention time (HRT), leading to a larger bioreactor volume. In this study, polyurethane sponge sheets were provided in a six-compartment ABR for retention and growth of biomass to improve its treatment performance at shorter HRTs. Polyurethane sponge was selected for its low cost, durability, availability, easy emplacement, and high voidage. The sponge anaerobic baffled reactor (SABR) was operated within a temperature range of 35 ± 1 °C at HRTs of 18, 12, 8, and 6 h to evaluate its treatment performance. Average removal efficiencies ranged from 60–77% for organics, 74–81% for total suspended solids (TSS), 50–66% for total nitrogen (TN), and 47–57% for total phosphorus (TP). The shortest HRT was 8 h with average removal efficiencies of 74, 63, 64, and 52% for organics, TSS, TN, and TP, respectively, to meet effluent discharge limits. With the shortest HRT of 8 h, the SABR demonstrated low volume requirements, thereby making it an efficient solution for decentralized wastewater treatment, particularly advantageous for developing countries with warm climates. Full article
Show Figures

Figure 1

Figure 1
<p>Schematic diagram of experimental setup.</p>
Full article ">Figure 2
<p>COD removal profile during startup phase.</p>
Full article ">Figure 3
<p>COD removal profile during performance evaluation phase at various HRTs.</p>
Full article ">Figure 4
<p>Average COD removal performance at various HRTs and effluent COD permissible limit.</p>
Full article ">Figure 5
<p>Average TSS removal performance at various HRTs and effluent TSS permissible limit.</p>
Full article ">Figure 6
<p>Total nitrogen removal at various HRTs and effluent TN discharge permissible limits.</p>
Full article ">Figure 7
<p>Total phosphorus removal at various HRTs and effluent TP discharge permissible limit.</p>
Full article ">Figure 8
<p>Alkalinity and VFA/Alkalinity ratio at various HRTs.</p>
Full article ">Figure 9
<p>COD removal efficiency before and after the introduction of polyurethane sheets and the corresponding improvement in COD removal efficiency at various HRTs.</p>
Full article ">Figure 10
<p>TSS removal efficiency before and after the introduction of polyurethane sheets and the corresponding improvement in TSS removal efficiency at various HRTs.</p>
Full article ">
10 pages, 5682 KiB  
Article
Outstanding Potential for Treating Wastewater from Office Buildings Using Fixed Activated Sludge with Attached Growth Process
by Nguyen Nguyet Minh Phan, Quang Chi Bui, Trung Viet Nguyen, Chih-Chi Yang, Ku-Fan Chen and Yung-Pin Tsai
Sustainability 2024, 16(17), 7560; https://doi.org/10.3390/su16177560 - 31 Aug 2024
Viewed by 853
Abstract
The application of fixed activated sludge with an attached growth process (FASAG) with optimal operating conditions (hydraulic retention time (HRT) of 7 h, dissolved oxygen (DO) of 6 mg/L, and alkalinity dosage of 7.14 mgCaCO3/mgN-NH4+) treats wastewater generated [...] Read more.
The application of fixed activated sludge with an attached growth process (FASAG) with optimal operating conditions (hydraulic retention time (HRT) of 7 h, dissolved oxygen (DO) of 6 mg/L, and alkalinity dosage of 7.14 mgCaCO3/mgN-NH4+) treats wastewater generated from office buildings to meet discharge requirements (as per the regulation in the nation where the study was conducted) with typical parameters such as pH of 6.87–7.56, chemical oxygen demand (COD) of 32–64 mg/L, suspended solids (SS) of 8–11 mg/L, N-NH4+ of 1–7 mg/L, and denitrification efficiency reaches 53%. In addition, the FASAG is an outstanding integration that makes both economic and environmental sense when applied in local wastewater treatment systems. In particular, this process combines aerobic and anoxic processes in a creation tank. This explains why this approach can save investment and operating costs, energy, and land funds. In office building regions, where land area is frequently limited, saving land funds presents numerous options to enhance the density of green cover. Furthermore, as a new aspect, investing in reusing wastewater after treatment to irrigate plants or flush toilets in office buildings contributes to a decrease in the quantity of wastewater released into the environment, saving water resources and supporting sustainable development. Full article
Show Figures

Figure 1

Figure 1
<p>Experimental device.</p>
Full article ">Figure 2
<p>The biofilm carrier materials used in research.</p>
Full article ">Figure 3
<p>pH values during the experiment.</p>
Full article ">Figure 4
<p>Frequency of appearance of influent COD concentration.</p>
Full article ">Figure 5
<p>Effective COD treatment.</p>
Full article ">Figure 6
<p>Red worms form in the treatment reactor.</p>
Full article ">Figure 7
<p>Effective SS treatment.</p>
Full article ">Figure 8
<p>Effective ammonia treatment.</p>
Full article ">Figure 9
<p>Frequency of ammonia appearance in influent wastewater.</p>
Full article ">Figure 10
<p>Effective nitrate removal.</p>
Full article ">Figure 11
<p>Ratio between ammonia concentration and required alkalinity.</p>
Full article ">
23 pages, 3806 KiB  
Article
Continuous UV/H2O2 Process: A Sustainable Wastewater Treatment Approach for Enhancing the Biodegradability of Aqueous PVA
by Zahra Parsa, Ramdhane Dhib and Mehrab Mehrvar
Sustainability 2024, 16(16), 7060; https://doi.org/10.3390/su16167060 - 17 Aug 2024
Viewed by 861
Abstract
Implementing efficient and cost-effective wastewater treatment methods in wastewater treatment plants (WWTPs) is crucial for ensuring sustainable development in contemporary societies. This study explores the feasibility of a continuous UV/H2O2 tubular photoreactor as a pre-treatment to enhance the biodegradability [...] Read more.
Implementing efficient and cost-effective wastewater treatment methods in wastewater treatment plants (WWTPs) is crucial for ensuring sustainable development in contemporary societies. This study explores the feasibility of a continuous UV/H2O2 tubular photoreactor as a pre-treatment to enhance the biodegradability of aqueous polyvinyl alcohol (PVA) solutions, known as a nonbiodegradable wastewater. Using a combination of a Box–Behnken design (BBD) and the response surface methodology (RSM), three main process variables, including the PVA feed concentration, the inlet H2O2 concentration, and the PVA feed flow rate, are studied within ranges of 500–1500 mg/L, 390–780 mg/L, and 50–150 mL/min, respectively. The results show significant interaction effects between the PVA feed and inlet H2O2 concentrations on the effluent BOD5/COD ratio. The optimal operating conditions are determined using the RSM, with a PVA feed concentration of 665 mg/L, an inlet H2O2 concentration of 390 mg/L, and a PVA feed flow rate of 59 mL/min. Operating at this point leads to an increase in the effluent BOD5/COD ratio from 0.15 to 0.53, which is validated experimentally with a ±5% error. Under these conditions, the effluent demonstrates an enhanced biodegradability, allowing for redirection to a subsequent biological post-treatment phase. This study demonstrates that using the UV/H2O2 process to enhance the biodegradability of an aqueous PVA solution is more economical than focusing on the complete removal of total organic carbon (TOC). Also, a comparison of these results with those of our previous study indicates that wastewater becomes more biodegradable by progressing the UV/H2O2 process due to the breakdown of polymer molecules, which reduces their molecular weight and makes them more consumable for biomass. Full article
Show Figures

Graphical abstract

Graphical abstract
Full article ">Figure 1
<p>Schematic diagram of the lab-scale continuous UV/H<sub>2</sub>O<sub>2</sub> system.</p>
Full article ">Figure 2
<p>Cumulative oxygen uptake (mg/L) by degrading microorganisms over time (h) in low-rate batch respirometry tests for solutions containing different concentrations of PVA compared to a control reference in the presence of activated sludge at 20 °C and in agitated condition.</p>
Full article ">Figure 3
<p>Comparison of observed effluent BOD<sub>5</sub>/COD with the predicted values by the model.</p>
Full article ">Figure 4
<p>Influence of (<b>a</b>) the PVA feed concentration, (<b>b</b>) the inlet H<sub>2</sub>O<sub>2</sub> concentration, and (<b>c</b>) the PVA feed flow rate on the effluent BOD<sub>5</sub>/COD, while the other two variables are kept constant at their central design values.</p>
Full article ">Figure 5
<p>Inner dimensions of the photoreactor: E<sub>0</sub>: UV light incident irradiance adjacent to the lamp (sleeve is neglected); and E<sub>r</sub>: UV light irradiance adjacent to the photoreactor’s wall at a radial distance of r = 1.25 cm from the UV lamp.</p>
Full article ">Figure 6
<p>Influence of average UV fluence at 254 nm (J/m<sup>2</sup>) on the effluent BOD<sub>5</sub>/COD, while PVA feed and inlet H<sub>2</sub>O<sub>2</sub> concentrations were kept constant at 1000 and 585 mg/L, respectively, corresponding to their central design values.</p>
Full article ">Figure 7
<p>Response surface plots of process variables in UV/H<sub>2</sub>O<sub>2</sub> process. Interaction effects of (<b>a</b>) PVA feed and inlet H<sub>2</sub>O<sub>2</sub> concentrations, (<b>b</b>) PVA feed concentration and flow rate, and (<b>c</b>) inlet H<sub>2</sub>O<sub>2</sub> concentration and PVA feed flow rate on the effluent BOD<sub>5</sub>/COD.</p>
Full article ">Figure 7 Cont.
<p>Response surface plots of process variables in UV/H<sub>2</sub>O<sub>2</sub> process. Interaction effects of (<b>a</b>) PVA feed and inlet H<sub>2</sub>O<sub>2</sub> concentrations, (<b>b</b>) PVA feed concentration and flow rate, and (<b>c</b>) inlet H<sub>2</sub>O<sub>2</sub> concentration and PVA feed flow rate on the effluent BOD<sub>5</sub>/COD.</p>
Full article ">
26 pages, 5275 KiB  
Article
Adsorption of a Multicomponent Pharmaceutical Wastewater on Charcoal-Based Activated Carbon: Equilibrium and Kinetics
by Mina Asheghmoalla and Mehrab Mehrvar
Water 2024, 16(15), 2086; https://doi.org/10.3390/w16152086 - 24 Jul 2024
Viewed by 1276
Abstract
The treatment of pharmaceutical wastewater is a critical environmental challenge, necessitating efficient removal methods. This study investigates the adsorption of a synthetic multicomponent pharmaceutical wastewater (SPWW) containing methanol, benzene, methylene chloride, 4-aminophenol, aniline, and sulfanilic acid onto charcoal-based activated carbon (AC). Batch experiments [...] Read more.
The treatment of pharmaceutical wastewater is a critical environmental challenge, necessitating efficient removal methods. This study investigates the adsorption of a synthetic multicomponent pharmaceutical wastewater (SPWW) containing methanol, benzene, methylene chloride, 4-aminophenol, aniline, and sulfanilic acid onto charcoal-based activated carbon (AC). Batch experiments were conducted to study the effects of pH, contact time, and initial concentrations of the adsorbates. The results show that longer contact time and higher initial concentrations increase the adsorption capacity, whereas pH shows no significant effect on the adsorption capacity at a value of less than 10, eliminating the need for pH adjustment and reducing process costs. The pseudo-second order (PSO) kinetic model best describes the adsorption process, with intraparticle diffusion playing a key role, as confirmed by the Weber and Morris (W-M) model. Six models describing the adsorption at equilibrium are applied to experimental data, and their parameters are estimated with a nonlinear regression model. Among isotherm models, the Langmuir-Freundlich model provides the best fit, suggesting multilayer adsorption on a heterogeneous granular activated carbon (GAC) surface. The maximum adsorption capacity is estimated to be 522.3 mgC/gAC. Experimental results confirm that GAC could effectively treat highly concentrated pharmaceutical wastewater, achieving up to 52% removal efficiency. Full article
Show Figures

Graphical abstract

Graphical abstract
Full article ">Figure 1
<p>Variation in the adjusted volume of adsorbed nitrogen (V<sub>adsorbed</sub>) on granular activated carbon (GAC) by changing nitrogen gas pressures (P) at 273 K and 1 atm. The adsorption and desorption isotherms are obtained from Brunauer-Emmett-Teller (BET) surface analyzer at saturation pressure (P<sub>0</sub>) of 101.8 kPa and temperature of 77 K.</p>
Full article ">Figure 2
<p>Distribution of differential GAC pore volume with respect to its pore width (D) obtained from BET surface analyzer with BJH method using nitrogen gas desorption at <math display="inline"><semantics> <mrow> <mi mathvariant="normal">T</mi> <mo>=</mo> <mn>77</mn> <mrow> <mo> </mo> <mi mathvariant="normal">K</mi> </mrow> </mrow> </semantics></math>.</p>
Full article ">Figure 3
<p>The observed change in pH (<math display="inline"><semantics> <mrow> <mo mathvariant="normal">Δ</mo> <mi>pH</mi> </mrow> </semantics></math>) of 0.01 M NaCl solution after 24 h by varying its initial pH, following the pH drift method to determine the point zero charge (pH<sub>PZC</sub>) of GAC. GAC dosage = 3 gAC/L, T = 23 °C, shaking speed = 150 rpm.</p>
Full article ">Figure 4
<p>Effect of synthetic pharmaceutical wastewater initial pH on TOC removal by adsorption on GAC under batch mode after 24 h. TOC<sub>0</sub> = 1170.7 mgC/L, adsorbent dosage = 1 gAC/L, T = 23 °C, shaking speed = 150 rpm.</p>
Full article ">Figure 5
<p>Effect of contact time and initial TOC of synthetic pharmaceutical wastewater on adsorption capacity of GAC in batch mode. Adsorbent dosage = 1 gAC/L, T = 23 °C, and shaking speed = 150 rpm.</p>
Full article ">Figure 6
<p>Experimental data and kinetic models showing GAC capacity (q<sub>t</sub>) by varying the contact time for pharmaceutical removal from wastewater in batch mode. TOC<sub>0</sub> = 963.3 mgC/L, adsorbent dosage = 1 gAC/L, T = 23 °C, and shaking speed = 150 rpm.</p>
Full article ">Figure 7
<p>Weber and Morris intraparticle diffusion model for pharmaceutical adsorption from wastewater on GAC under batch mode. Average TOC<sub>0</sub> = 963.3 mgC/L, adsorbent dosage = 1 gAC/L, T = 23 °C, and shaking speed = 150 rpm.</p>
Full article ">Figure 8
<p>Freundlich isotherm linear plot for treatment of multicomponent synthetic pharmaceutical wastewater by adsorption on GAC after 24 h in batch mode. Average TOC<sub>0</sub> = 911.8 mgC/L, T = 23 °C, and shaking speed = 150 rpm.</p>
Full article ">Figure 9
<p>Change in the GAC equilibrium adsorption capacity by varying the equilibrium TOC of multicomponent synthetic pharmaceutical wastewater for the Experimental data points and six fitted isotherm models for batch-mode treatment after 24 h of contact time. Average TOC<sub>0</sub> = 911.8 mgC/L, T = 23 °C, and shaking speed = 150 rpm.</p>
Full article ">
16 pages, 3553 KiB  
Article
Sustainable Sludge Management in China: Quantifying GHG Emissions and Exploring Its Reduction Strategies
by Dongming Hu, Peng Jiang, Yipei Chen, Fuyan Gao and Shuai Liu
Processes 2024, 12(7), 1481; https://doi.org/10.3390/pr12071481 - 15 Jul 2024
Viewed by 1165
Abstract
This study aims to evaluate the emissions of greenhouse gases (GHGs) stemming from the sludge treatment sector in China and to investigate the feasibility of novel technologies in curtailing these emissions, with the aim of fostering sustainable sludge management methodologies. Employing a life-cycle [...] Read more.
This study aims to evaluate the emissions of greenhouse gases (GHGs) stemming from the sludge treatment sector in China and to investigate the feasibility of novel technologies in curtailing these emissions, with the aim of fostering sustainable sludge management methodologies. Employing a life-cycle assessment (LCA) methodology, the research computed the comprehensive GHG emissions resulting from sludge treatment, taking into consideration diverse elements such as treatment techniques (e.g., landfills, incineration, and land application) and the geographical variations among China’s 660 municipalities. Findings indicate that the total amount of GHG emissions from sludge treatment amounted to 18.54 Mt CO2-eq in 2017, with incineration registering the highest emissions (10,011.53 kg CO2-eq/t dry sludge (DS)), followed by landfills (717.51 kg CO2-eq/t DS) and land application (276.41 kg CO2-eq/t DS). The geographical dispersion of emissions characteristics reveal notable regional disparities, with the top 1% of cities responsible for 34.2% of the overall emissions. The concentration of emissions in the top 1 percent of cities underscores the necessity for tailored mitigation measures that consider localized sustainable development challenges. Principal component analysis (PCA) demonstrates that economic determinants and treatment scales exert substantial influence on emissions, underscoring the imperative of aligning Sustainable Development Goals (SDGs) with economic advancement. To curtail the carbon footprint associated with sludge treatment and enhance sustainability, the study evaluated the emission mitigation potential and expenses of diverse technologies, encompassing thermal conversion, anaerobic digestion, hydrothermal treatment, and wet oxidation. These technologies have the capacity to slash GHG emissions by 0.09–0.46 t CO2-eq/t DS in comparison to traditional approaches, while concurrently advancing resource recuperation and principles of circular economy. For instance, gasification could diminish GHG emissions by 0.33–0.46 t CO2-eq/t DS, whereas anaerobic digestion could yield reductions of 0.09–0.30 t CO2-eq/t DS. The implementation of these innovative technologies across 660 Chinese municipalities could potentially curtail total GHG emissions from sludge treatment by 15–40%. Nevertheless, further enhancements are imperative to refine their environmental and economic efficiency and guarantee enduring sustainability. By deploying these technologies and embracing optimization tactics, China’s sludge treatment sector can make a substantial contribution towards attaining national carbon neutrality objectives and advancing sustainable development. Full article
Show Figures

Figure 1

Figure 1
<p>System boundary to describe GHG emissions from the sludge treatment industry.</p>
Full article ">Figure 2
<p>Treated sludge produced in 31 provinces [<a href="#B20-processes-12-01481" class="html-bibr">20</a>].</p>
Full article ">Figure 3
<p>GHG emission from various sources from three sludge treatment techniques.</p>
Full article ">Figure 4
<p>Provincial GHG emission characteristics from sludge treatment sector.</p>
Full article ">Figure 5
<p>Distributions of GHG emissions at city level.</p>
Full article ">Figure 6
<p>Principal component analysis.</p>
Full article ">
22 pages, 5766 KiB  
Article
Sustainable Catalysts from Industrial FeO Waste for Pyrolysis and Oxidation of Hospital Polypropylene in Cartagena
by Joaquín Hernandez-Fernandez, Juan Carrascal Sanchez and Juan Lopez Martinez
Sustainability 2024, 16(14), 5934; https://doi.org/10.3390/su16145934 - 11 Jul 2024
Viewed by 918
Abstract
During the COVID-19 pandemic, polypropylene waste generated in hospitals increased significantly. However, conventional strategies for the final disposal of environmental waste, such as incineration, proved inefficient due to the generation of toxic chemical species. In this research, these PP wastes were mixed with [...] Read more.
During the COVID-19 pandemic, polypropylene waste generated in hospitals increased significantly. However, conventional strategies for the final disposal of environmental waste, such as incineration, proved inefficient due to the generation of toxic chemical species. In this research, these PP wastes were mixed with 1.5, 20, 150, 200, and 400 mg of iron oxide (FeO), extruded, and pelletized to obtain samples HW-PP-0, HW-PP-1, HW-PP-2, HW-PP-3, and HW-PP-4, respectively. XRF, TGA, and GC-MS characterized these samples. The samples were subjected to pyrolysis and thermo-oxidative degradation with controlled currents of nitrogen and oxygen. The characterization of the gases resulting from pyrolysis was carried out with a GC-MS, where the results showed that HW-PP-0 (mixed with 1.5 mg of FeO) presented the highest concentrations of alkanes (35.65%) and alkenes (63.7%), and the lowest levels of alkynes (0.3%), alcohols (0.12%), ketones (0.04%), and carboxylic acids (0.2%). The opposite was observed with the hospital waste HW-PP-4 (mixed with 400 mg of FeO), which presented the highest levels of alkynes (2.93%), alcohols (28.1%), ketones (9.8%), and carboxylic acids (8%). The effect of FeO on HW-PP-O during thermo-oxidative degradation generated values of alkanes (11%) and alkenes (30%) lower than those during pyrolysis. The results showed the catalytic power of FeO and its linear relationship with concentration. This research proposes the mechanisms that can explain the formation of different functional groups of various molecular weights which allow us to understand the presence of alkanes, alkenes, alkynes, alcohols, ketones, and carboxylic acids. Full article
Show Figures

Figure 1

Figure 1
<p>Processing diagram.</p>
Full article ">Figure 2
<p>TGA (<b>A</b>) and dTGA (<b>B</b>) for PP with different amounts of iron oxide.</p>
Full article ">Figure 3
<p>(<b>a</b>) Trend graph for alkanes as a function of the amount of FeO; (<b>b</b>) trend graph for alkenes as a function of the amount of FeO; (<b>c</b>) trend graph for alkynes as a function of the amount of FeO; (<b>d</b>) trend graph for alcohols as a function of the amount of FeO; (<b>e</b>) trend graph for ketones as a function of the amount of FeO; (<b>f</b>) trend graph for acids as a function of the amount of FeO.</p>
Full article ">Figure 3 Cont.
<p>(<b>a</b>) Trend graph for alkanes as a function of the amount of FeO; (<b>b</b>) trend graph for alkenes as a function of the amount of FeO; (<b>c</b>) trend graph for alkynes as a function of the amount of FeO; (<b>d</b>) trend graph for alcohols as a function of the amount of FeO; (<b>e</b>) trend graph for ketones as a function of the amount of FeO; (<b>f</b>) trend graph for acids as a function of the amount of FeO.</p>
Full article ">Figure 4
<p>(<b>a</b>) Boxplot for alkanes; (<b>b</b>) boxplot for alkenes; (<b>c</b>) boxplot for ketones; (<b>d</b>) boxplot for alcohols; (<b>e</b>) boxplot for acids; (<b>f</b>) boxplot for alkynes.</p>
Full article ">Figure 4 Cont.
<p>(<b>a</b>) Boxplot for alkanes; (<b>b</b>) boxplot for alkenes; (<b>c</b>) boxplot for ketones; (<b>d</b>) boxplot for alcohols; (<b>e</b>) boxplot for acids; (<b>f</b>) boxplot for alkynes.</p>
Full article ">Figure 5
<p>Trends by families in an oxidative atmosphere.</p>
Full article ">Figure 6
<p>(<b>a</b>) Trend graph for alkanes in N<sub>2</sub> and O<sub>2</sub> atmospheres; (<b>b</b>) trend graph for alkenes in N<sub>2</sub> and O<sub>2</sub> atmospheres; (<b>c</b>) trend graph for alkynes in N<sub>2</sub> and O<sub>2</sub> atmospheres; (<b>d</b>) trend graph for alcohols in N<sub>2</sub> and O<sub>2</sub> atmospheres; (<b>e</b>) trend graph for ketones in N<sub>2</sub> and O<sub>2</sub> atmospheres; (<b>f</b>) trend graph for acids in N<sub>2</sub> and O<sub>2</sub> atmospheres.</p>
Full article ">Figure 7
<p>Diagram of products obtained by HPW pyrolysis.</p>
Full article ">Figure 8
<p>Thermal degradation of PP without a catalyst (FeO).</p>
Full article ">Figure 9
<p>Thermal degradation of PP with catalyst (FeO).</p>
Full article ">Figure 10
<p>Thermal degradation of PP with catalyst (FeO) and traces of air (O<sub>2</sub>).</p>
Full article ">Figure 11
<p>Pyrolysis, cracking, and deactivation of polypropylene under the influence of the FeO catalyst.</p>
Full article ">
11 pages, 1471 KiB  
Article
Recovery of Cleaning Solutions from Dairy Manufacturing Effluents Using Membrane Technology
by Izabela Kowalska
Sustainability 2024, 16(13), 5793; https://doi.org/10.3390/su16135793 - 8 Jul 2024
Viewed by 987
Abstract
The recovery concept of cleaning solutions, based on single-phase detergents from cleaning-in-place (CIP) effluents from the dairy industry, is presented. The first step consists of ultrafiltration (UF) (with a cut-off of 5 or 10 kDa) to reduce the high load of milk proteins, [...] Read more.
The recovery concept of cleaning solutions, based on single-phase detergents from cleaning-in-place (CIP) effluents from the dairy industry, is presented. The first step consists of ultrafiltration (UF) (with a cut-off of 5 or 10 kDa) to reduce the high load of milk proteins, followed by nanofiltration (NF) (with a cut-off of 200 Da) to separate low molecular weight lactose. Membrane steps were performed in the concentration mode, achieving a recovery of 75% of the solutions. UF modules reduced 70–85% of chemical oxygen demand (COD), 99% of milk proteins, and 45–70% of lactose, limiting the susceptibility of NF modules to fouling. Combined with nanofiltration, the efficiency of the purification system is 100% for proteins and more than 99% for lactose. The solutions recovered in the proposed purification variants are recognized as sodium hydroxide solutions with a surfactant admixture, and they can be successfully re-used for cleaning processes in the production plant. Full article
Show Figures

Figure 1

Figure 1
<p>Schematic diagram of the recovery of CIP solutions.</p>
Full article ">Figure 2
<p>Normalized flux of ultrafiltration modules depending on the recovery rate (C5: TMP = 3.0 bar, CFV = 4.4 m/s; C10: TMP = 3.0 bar, CFV = 3.8 m/s; PM5: TMP = 1.0 bar, CFV = 2.2 m/s).</p>
Full article ">Figure 3
<p>Normalized flux of nanofiltration modules depending on the recovery rate (AFC30: TMP = 4.0 bar, CFV = 0.6 m/s).</p>
Full article ">Figure 4
<p>Composition of the recovered cleaning solutions (C5: TMP = 3.0 bar, CFV = 4.4 m/s; C10: TMP = 3.0 bar, CFV = 3.8 m/s; PM5: TMP = 1.0 bar, CFV = 2.2 m/s; AFC30: TMP = 4.0 bar, CFV = 0.6 m/s).</p>
Full article ">Figure 4 Cont.
<p>Composition of the recovered cleaning solutions (C5: TMP = 3.0 bar, CFV = 4.4 m/s; C10: TMP = 3.0 bar, CFV = 3.8 m/s; PM5: TMP = 1.0 bar, CFV = 2.2 m/s; AFC30: TMP = 4.0 bar, CFV = 0.6 m/s).</p>
Full article ">
13 pages, 3523 KiB  
Article
Optimizing an Anaerobic Hybrid Reactor Series for Effective High-Strength Fresh Leachate Treatment and Biogas Generation
by Sakulrat Sutthiprapa, Sirintornthep Towprayoon, Chart Chiemchaisri, Pawinee Chaiprasert and Komsilp Wangyao
Sustainability 2024, 16(7), 3076; https://doi.org/10.3390/su16073076 - 7 Apr 2024
Cited by 1 | Viewed by 1856
Abstract
Treating high-strength fresh leachate is challenging and of great interest due to the inherent variability in its physical and chemical characteristics. This research aims to enhance the efficiency of the anaerobic hybrid reactor (AHR) series in treating high-strength fresh leachate and achieving biogas [...] Read more.
Treating high-strength fresh leachate is challenging and of great interest due to the inherent variability in its physical and chemical characteristics. This research aims to enhance the efficiency of the anaerobic hybrid reactor (AHR) series in treating high-strength fresh leachate and achieving biogas generation from fresh leachate at ambient temperatures. The AHR series used consists of two serially connected reactors termed the first anaerobic hybrid reactor (AHR-1) and the secondary anaerobic hybrid reactor (AHR-2). AHR-1 treated high-concentration fresh leachate with an organic loading rate (OLR) between 5 and 20 kgCOD/m3·d. AHR-2 treated the effluent from the first tank and removed organic matter from the system. The experiment was conducted for 210 days, showing that an OLR of 10 kgCOD/m3·d resulted in the most suitable COD removal efficiency, ranging from 82 to 91%. The most suitable OLR for biogas production was 15 kgCOD/m3·d. The AHR series proved to be an efficient system for treating high-strength fresh leachate and generating biogas, making it applicable to leachate treatment facilities at waste transfer stations and landfill sites. Treating leachate and utilizing it as a renewable energy source using the AHR series presents a practical and efficient waste management approach. High-strength leachate can be effectively treated with the AHR series; such methods may be integrated into industries treating leachates with high COD values. Full article
Show Figures

Figure 1

Figure 1
<p>Nylon fiber carriers in the AHR series system.</p>
Full article ">Figure 2
<p>AHR series schematic diagram.</p>
Full article ">Figure 3
<p>COD removal efficiencies of the AHR series at various OLRs.</p>
Full article ">Figure 4
<p>Relationships between (<b>a</b>) %COD removal and biogas production of the AHR series and (<b>b</b>) %COD removal and CH<sub>4</sub> production of the AHR series.</p>
Full article ">Figure 5
<p>Volatile suspended solids in the influent and effluent of AHR reactors.</p>
Full article ">Figure 6
<p>CH<sub>4</sub> contents (%) in (<b>a</b>) AHR-1 and (<b>b</b>) AHR-2.</p>
Full article ">Figure 7
<p>Relationships between (<b>a</b>) OLR and CH<sub>4</sub> yield of AHR-1, (<b>b</b>) OLR and CH<sub>4</sub> yield of AHR-2, and (<b>c</b>) OLR and CH<sub>4</sub> yield of the AHR series.</p>
Full article ">Figure 8
<p>Relationships between (<b>a</b>) OLR and biogas production in the AHR series and (<b>b</b>) OLR and CH<sub>4</sub> production in the AHR series.</p>
Full article ">
44 pages, 6980 KiB  
Review
Dynamic Modelling, Process Control, and Monitoring of Selected Biological and Advanced Oxidation Processes for Wastewater Treatment: A Review of Recent Developments
by Zahra Parsa, Ramdhane Dhib and Mehrab Mehrvar
Bioengineering 2024, 11(2), 189; https://doi.org/10.3390/bioengineering11020189 - 16 Feb 2024
Cited by 4 | Viewed by 2631
Abstract
This review emphasizes the significance of formulating control strategies for biological and advanced oxidation process (AOP)-based wastewater treatment systems. The aim is to guarantee that the effluent quality continuously aligns with environmental regulations while operating costs are minimized. It highlights the significance of [...] Read more.
This review emphasizes the significance of formulating control strategies for biological and advanced oxidation process (AOP)-based wastewater treatment systems. The aim is to guarantee that the effluent quality continuously aligns with environmental regulations while operating costs are minimized. It highlights the significance of understanding the dynamic behaviour of the process in developing effective control schemes. The most common process control strategies in wastewater treatment plants (WWTPs) are explained and listed. It is emphasized that the proper control scheme should be selected based on the process dynamic behaviour and control goal. This study further discusses the challenges associated with the control of wastewater treatment processes, including inadequacies in developed models, the limitations of most control strategies to the simulation stage, the imperative requirement for real-time data, and the financial and technical intricacies associated with implementing advanced controller hardware. It is discussed that the necessity of the availability of real-time data to achieve reliable control can be achieved by implementing proper, accurate hardware sensors in suitable locations of the process or by developing and implementing soft sensors. This study recommends further investigation on available actuators and the criteria for choosing the most appropriate one to achieve robust and reliable control in WWTPs, especially for biological and AOP-based treatment approaches. Full article
Show Figures

Graphical abstract

Graphical abstract
Full article ">Figure 1
<p>Classification of major biological wastewater treatment processes (adapted from [<a href="#B7-bioengineering-11-00189" class="html-bibr">7</a>,<a href="#B8-bioengineering-11-00189" class="html-bibr">8</a>,<a href="#B9-bioengineering-11-00189" class="html-bibr">9</a>]).</p>
Full article ">Figure 2
<p>Different AOPs involving ROS (adapted from [<a href="#B15-bioengineering-11-00189" class="html-bibr">15</a>]).</p>
Full article ">Figure 3
<p>Classification of different AOPs (adapted from [<a href="#B26-bioengineering-11-00189" class="html-bibr">26</a>]).</p>
Full article ">Figure 4
<p>Black-box system identification diagram for capturing the dynamic behaviour of a system. The known input, u(t), can be sinusoidal, pulse, step, or pseudo-random binary sequence (PRBS), resulting in process output y(t) as frequency response, pulse response, or process reaction curve.</p>
Full article ">Figure 5
<p>Different model structures of system identification: <sup>a</sup> autoregressive with eXogenous input model; <sup>b</sup> Hammerstein–Wiener model; <sup>c</sup> non-linear AutoRegressive with eXogenous input model (adapted from [<a href="#B37-bioengineering-11-00189" class="html-bibr">37</a>,<a href="#B38-bioengineering-11-00189" class="html-bibr">38</a>]).</p>
Full article ">Figure 6
<p>General flowchart of system identification technique.</p>
Full article ">
29 pages, 13339 KiB  
Article
Model-Based Construction of Wastewater Treatment Plant Influent Data for Simulation Studies
by Jens Alex
Water 2024, 16(4), 564; https://doi.org/10.3390/w16040564 - 13 Feb 2024
Cited by 1 | Viewed by 2256
Abstract
The quality of simulations for wastewater treatment plants is heavily dependent on the quality of the simulation input data. Inflow data from wastewater treatment plants collected by measurement cannot usually be used directly for a wastewater treatment plant simulation. A method is presented [...] Read more.
The quality of simulations for wastewater treatment plants is heavily dependent on the quality of the simulation input data. Inflow data from wastewater treatment plants collected by measurement cannot usually be used directly for a wastewater treatment plant simulation. A method is presented with which dynamic inflow descriptions for simulation studies can be generated from typical operational measurements. These are volume-proportional 24 h composite samples and continuously recorded inflow water flow rates. To derive the method, a deterministic model was first developed to describe typical dry weather daily inflow concentration patterns and validated for a larger number of measured daily inflow measurements (2 h composite samples). In the second part of the article, the method is then developed with which the dynamic wastewater treatment plant inflow can be calculated for a longer period of time from the modelled dry weather daily inflow and a high-resolution time series of measured flow rates. This dynamic inflow can be used to validate wastewater treatment plant models if additional online measurements for effluent concentrations (e.g., NH4-N and NO3-N) are available. The proposed method is highly suitable for calculating an online estimate of the influent concentrations, which can be used as input information for digital twins, such as observer models and predictive controllers, based solely on the online measurement of the influent flow rate. Full article
Show Figures

Graphical abstract

Graphical abstract
Full article ">Figure 1
<p>Modelling approach for dry weather inflow Langergraber et al. 2008 [<a href="#B5-water-16-00564" class="html-bibr">5</a>].</p>
Full article ">Figure 2
<p>Fourier approximation of the dry weather inflow Langergraber et al. 2008 [<a href="#B5-water-16-00564" class="html-bibr">5</a>].</p>
Full article ">Figure 3
<p>Dry weather influent block in SIMBA<sup>#</sup>.</p>
Full article ">Figure 4
<p>Setting the shape parameters.</p>
Full article ">Figure 5
<p>Setting the concentrations.</p>
Full article ">Figure 6
<p>Inlet flow data with dry weather period.</p>
Full article ">Figure 7
<p>Inlet divided into additional infiltration water, infiltration water, urine, grey water, and rainwater runoff.</p>
Full article ">Figure 8
<p>Inflow calculation in the SIMBA block “Influent Generator 2023”.</p>
Full article ">Figure 9
<p>Automatic adjustment of the form parameters.</p>
Full article ">Figure 10
<p>Self-documentation from block TG_caseC.</p>
Full article ">Figure 11
<p>Reproduction of daily pattern, variant 2023 (selection). The legends for measured Q and measured COD include the id (1–21) of the analysed sample plant. See <a href="#app3-water-16-00564" class="html-app">Appendix C</a> for all analysed data sets.</p>
Full article ">Figure 11 Cont.
<p>Reproduction of daily pattern, variant 2023 (selection). The legends for measured Q and measured COD include the id (1–21) of the analysed sample plant. See <a href="#app3-water-16-00564" class="html-app">Appendix C</a> for all analysed data sets.</p>
Full article ">Figure 12
<p>Shape parameter wastewater flow rate as a function of plant size (PE). (A linear regression line is plotted as grey dotted line which appears as solid grey line in the plots).</p>
Full article ">Figure 13
<p>Shape parameter COD pattern. (A linear regression line is plotted as grey dotted line which appears as solid grey line in the plots).</p>
Full article ">Figure 14
<p>Resulting <math display="inline"><semantics> <mrow> <mi>C</mi> <mi>O</mi> <mi>D</mi> </mrow> </semantics></math> concentrations in the wastewater. (A linear regression line is plotted as grey dotted line which appears as solid grey line in the plots).</p>
Full article ">Figure 15
<p>Shape parameter for <span class="html-italic">TKN</span> pattern. (A linear regression line is plotted as grey dotted line which appears as solid grey line in the plots).</p>
Full article ">Figure 16
<p>Shape parameter <span class="html-italic">P</span> pattern. (A linear regression line is plotted as grey dotted line which appears as solid grey line in the plots).</p>
Full article ">Figure 17
<p>Synthetic inflow data (NH<sub>4</sub>-N load in kg/d) compared with measured data.</p>
Full article ">Figure A1
<p>Shape parameters.</p>
Full article ">Figure A2
<p>Model Fit for the Sample Diurnal Pattern (Complete results).</p>
Full article ">Figure A2 Cont.
<p>Model Fit for the Sample Diurnal Pattern (Complete results).</p>
Full article ">Figure A2 Cont.
<p>Model Fit for the Sample Diurnal Pattern (Complete results).</p>
Full article ">Figure A2 Cont.
<p>Model Fit for the Sample Diurnal Pattern (Complete results).</p>
Full article ">Figure A2 Cont.
<p>Model Fit for the Sample Diurnal Pattern (Complete results).</p>
Full article ">
37 pages, 931 KiB  
Review
Integrated and Hybrid Processes for the Treatment of Actual Wastewaters Containing Micropollutants: A Review on Recent Advances
by Mina Asheghmoalla and Mehrab Mehrvar
Processes 2024, 12(2), 339; https://doi.org/10.3390/pr12020339 - 5 Feb 2024
Cited by 4 | Viewed by 2666
Abstract
The global concern regarding the release of micropollutants (MPs) into the environment has grown significantly. Considerable amounts of persistent micropollutants are present in industrial discharges. Depending solely on a singular treatment approach is inadequate for the effective removal of MPs from wastewater due [...] Read more.
The global concern regarding the release of micropollutants (MPs) into the environment has grown significantly. Considerable amounts of persistent micropollutants are present in industrial discharges. Depending solely on a singular treatment approach is inadequate for the effective removal of MPs from wastewater due to their complex composition. The performance of different treatment methods to meet the discharge standards has been widely studied. These efforts are classified as hybrid and sequential processes. Despite their adequate performance, the optimization and industrial application of these methods could be challenging and costly. This review focuses on integrated (sequential) and hybrid processes for MP removal from actual wastewater. Furthermore, to provide a thorough grasp of the treatment approaches, the operational conditions, the source of wastewater containing MPs, and its characteristics are detailed. It is concluded that the optimal sequence to achieve the removal of MPs involves biological treatment followed by an advanced oxidation process (AOP) with a final passage through an activated carbon column. To refine this process further, a membrane unit could be added based on the desired effluent quality. Nevertheless, considering practical feasibility, this study identifies specific areas requiring additional research to implement this integrated treatment strategy effectively. Full article
Show Figures

Graphical abstract

Graphical abstract
Full article ">Figure 1
<p>Classification of advanced oxidation processes (adapted from [<a href="#B105-processes-12-00339" class="html-bibr">105</a>]).</p>
Full article ">
17 pages, 2818 KiB  
Article
Valorization of Acid Leaching Post-Consumer Gypsum Purification Wastewater
by Miguel Castro-Díaz, Sergio Cavalaro, Mohamed Osmani, Saeed Morsali, Matyas Gutai, Paul Needham, Bill Parker and Tatiana Lovato
Sustainability 2024, 16(1), 425; https://doi.org/10.3390/su16010425 - 3 Jan 2024
Viewed by 1529
Abstract
Industries are required to utilize treatment technologies to reduce contaminants in wastewater prior to discharge and to valorize by-products to increase sustainability and competitiveness. Most acid leaching gypsum purification studies have obviated the treatment of the highly acidic wastewater produced. In this work, [...] Read more.
Industries are required to utilize treatment technologies to reduce contaminants in wastewater prior to discharge and to valorize by-products to increase sustainability and competitiveness. Most acid leaching gypsum purification studies have obviated the treatment of the highly acidic wastewater produced. In this work, acidic wastewater from acid leaching purification of post-consumer gypsum was treated to recover a valuable solid product and reusable water. The main aims of this work were to determine the impact of recirculating acidic and treated wastewaters on the efficiency of the acid leaching purification process and to valorize the impurities in the wastewater. Samples were characterized through X-ray fluorescence and X-ray diffraction. SimaPro 9.5 and the ReCiPe 2016 midpoint method were used for the life cycle assessment of three sustainable wastewater management approaches. The reuse of the acidic wastewater did not improve the chemical purity of gypsum. Soluble impurities were precipitated at pH 10.5 as a magnesium-rich gypsum that could be commercialized as fertilizer or soil ameliorant. The alkaline-treated water was reused for six acid leaching purification cycles without impacting the efficiency of the purification process. An acid leaching–neutralization–filtration–precipitation approach demonstrated superior overall environmental performance. Barriers and enabling measures for the implementation of an in-house wastewater treatment were identified. Full article
Show Figures

Figure 1

Figure 1
<p>Schematic representation of the steps of the three sustainable wastewater management approaches (WMAs) investigated in this work.</p>
Full article ">Figure 2
<p>Chemical purity of gypsum from demolition plasterboard waste (GDPW) before and after acid leaching purification at 90 °C for 1 h using fresh and spent 5 wt% H<sub>2</sub>SO<sub>4</sub> solutions and a stirring rate of 150 rpm.</p>
Full article ">Figure 3
<p>Precipitate composition as a function of the final pH after neutralization of acidic wastewater obtained after one acid leaching purification cycle using fresh municipal water.</p>
Full article ">Figure 4
<p>Composition of the precipitates produced at pH 10.5 from acidic wastewater obtained after acid leaching purification of gypsum from refurbishment plasterboard waste (GRPW) and gypsum from demolition plasterboard waste (GDPW) at 90 °C for 1 h using a 5 wt% H<sub>2</sub>SO<sub>4</sub> solution prepared with municipal water and a stirring rate of 50 rpm. Only constituents with contents ≥1 wt% are displayed.</p>
Full article ">Figure 5
<p>Chemical purity of GDPW (<b>top</b>) and GRPW (<b>bottom</b>) after acid leaching purification at 90 °C for 2 h using a 3 wt% H<sub>2</sub>SO<sub>4</sub> solution prepared with purified water when using GDPW, municipal water when using GRPW, treated waters, and a stirring rate of 50 rpm.</p>
Full article ">Figure 6
<p>Comparison of the chemical purity of GRPW after acid leaching at 90 °C for 1 h using a 5 wt% H<sub>2</sub>SO<sub>4</sub> solution prepared with purified water and a stirring rate of 50 rpm after washing the gypsum cake with purified water during filtration and after neutralization of the gypsum slurry with Ca(OH)<sub>2</sub> to pH 5.5 prior to filtration.</p>
Full article ">Figure 7
<p>Chemical purity of GRPW after acid leaching at 90 °C for 2 h using 3 wt% H<sub>2</sub>SO<sub>4</sub> solutions prepared with municipal water using a stirring rate of 50 rpm after neutralization with Ca(OH)<sub>2</sub> to pH 5.5 (triplicate tests).</p>
Full article ">Figure 8
<p>Roadmap of sustainable wastewater management approach 3.</p>
Full article ">
13 pages, 4416 KiB  
Article
Factors Affecting the Morphology of Granular Sludge in Phosphorus-Accumulating Organism (PAO) and Denitrifying PAO (DPAO) Sequencing Batch Reactors
by Geumhee Yun, Zuwhan Yun, Young Kim and Kyungjin Han
Water 2023, 15(23), 4108; https://doi.org/10.3390/w15234108 - 27 Nov 2023
Viewed by 1442
Abstract
This study aimed to investigate the influencing factors and characteristics of granule morphology through approximately 500 d of long-term monitoring of two types of anaerobic–aerobic phosphorus-accumulating organism (PAO) and anaerobic–anoxic denitrifying PAO (DPAO) sequencing batch reactors (SBRs). The results show that granules were [...] Read more.
This study aimed to investigate the influencing factors and characteristics of granule morphology through approximately 500 d of long-term monitoring of two types of anaerobic–aerobic phosphorus-accumulating organism (PAO) and anaerobic–anoxic denitrifying PAO (DPAO) sequencing batch reactors (SBRs). The results show that granules were present in the DPAO SBR and PAO SBR after 200 d and 250 d of operation, respectively. The average diameters of the granules were 2.2 ± 0.7 mm in the DPAO SBR and 0.4 ± 0.3 mm in the PAO SBR, respectively. The DPAO granular sludge contained rod-shaped microorganisms, whereas the PAO granular sludge contained cocci-type microorganisms. A precipitated core consisting of hydroxyapatite was found in the DPAO granules. A comparative analysis conducted under various operating conditions revealed that the availability and type of the electron acceptors (EAs) may have a significant impact on granulation. This observation suggests that the presence and diversity of EAs are crucial factors for the development of different granule sizes and morphologies. Full article
Show Figures

Figure 1

Figure 1
<p>Images of granules in (<b>a</b>) the DPAO SBR and (<b>b</b>) the PAO SBR after 200 d of operation.</p>
Full article ">Figure 2
<p>Optical images of DPAO granules after 370 d of operation.</p>
Full article ">Figure 3
<p>Saturation index calculations for different minerals in the supernatant were performed for each pH (Minteq. ver. 3.1).</p>
Full article ">Figure 4
<p>EPS concentrations in the EPSs (<b>a</b>) and SMP (<b>b</b>) in both SBRs.</p>
Full article ">Figure 5
<p>The relationship between the granule size and H/D ratio (<b>a</b>), Aeration intensity (<b>b</b>), OLR (<b>c</b>), F/M ratio (<b>d</b>), HRT (<b>e</b>) and SRT (<b>f</b>) obtained from 34 references was compared with our results.</p>
Full article ">Figure 6
<p>The relationship between the granule size and settling time (<b>a</b>), SVI (<b>b</b>), MLSS (<b>c</b>) and EPS concentration (<b>d</b>) obtained from 34 references was compared with our results.</p>
Full article ">Figure 7
<p>Comparison of various characteristics of biological granules. Bars represent the range of the granule size, while open circles denote the averaged granule diameters extracted from 34 references (34 references are listed in <a href="#app1-water-15-04108" class="html-app">Table S2</a>).</p>
Full article ">
21 pages, 2412 KiB  
Article
Prediction of Leachate Characteristics via an Analysis of the Solubilized Extract of the Organic Fraction of Domestic Solid Waste from the Municipality of Belém, PA
by Diogo Oliveira Pereira, Fernanda Paula da Costa Assunção, Jéssica Cristina Conte da Silva, Jorge Fernando Hungria Ferreira, Raise Brenda Pinheiro Ferreira, Ádila Lima Lola, Ísis Costa Pereira do Nascimento, Jean Pinheiro Chaves, Mel Safira Cruz do Nascimento, Thalia da Silva Gouvêa, Neyson Martins Mendonça, Isaque Wilkson de Sousa Brandão, José Almir Rodrigues Pereira and Nélio Teixeira Machado
Sustainability 2023, 15(21), 15456; https://doi.org/10.3390/su152115456 - 30 Oct 2023
Cited by 2 | Viewed by 1277
Abstract
This work aimed to predict the physical–chemical characteristics of leachate according to the analysis of the solubilized extract from urban household solid waste (UHSW), on a laboratory scale, in the city of Belém/PA, Brazil. The neighborhoods where the waste was collected were sectorized [...] Read more.
This work aimed to predict the physical–chemical characteristics of leachate according to the analysis of the solubilized extract from urban household solid waste (UHSW), on a laboratory scale, in the city of Belém/PA, Brazil. The neighborhoods where the waste was collected were sectorized based on geographic and socioeconomic data, with family income as the main parameter. After collection, the material was sent to the segregation area, where a gravimetric analysis of the UHSW was performed and fractions (paper, cardboard, Tetra Pak, rigid plastic, malleable plastic, metals, glass, organic matter, sanitary waste, fabrics and rejects) were segregated. After the gravimetric characterization, it was found that the highest average proportions were 55.57% organic matter, 14.26% sanitary waste and 9.97% malleable plastic. The organic fraction was selected and subjected to drying, crushing, sieving and packaging pretreatment, and then the solubilized extract of this fraction was obtained according to NBR No. 10.006/2004 of the Brazilian Association of Technical Standards. In the analyses of the solubilized extract, values for total nitrogen (201.80 to 359.90 mg·L−1), ammonia nitrogen (161 to 289 mg·L−1), nitrate (10 to 40 mg·L−1) and chemical oxygen demand were obtained (28,701 mg·L−1 to 38,608 mg·L−1), indicating the similarity of the waste solubilization conditions to those of leachate from landfills, in addition to being in noncompliance with environmental and health legislation, thus making it necessary to have an efficient waste management system, which avoids the release of waste into the environment that would result in environmental impacts similar to those of leachate contact with the environment. Full article
Show Figures

Figure 1

Figure 1
<p>Process flowsheet of collection, classification/segregation and pretreatment of the organic fraction of MSW and obtainment of the solubilized extract.</p>
Full article ">Figure 2
<p>Neighborhoods served by Terraplena in Belém.</p>
Full article ">Figure 3
<p>Procedure for obtaining the solubilized extract.</p>
Full article ">Figure 4
<p>Proportions of waste fractions collected in the municipality of Belém.</p>
Full article ">Figure 5
<p>Comparison between the color and turbidity values of the solubilized extract obtained in relation to the regions delimited in the methodology.</p>
Full article ">Figure 6
<p>Concentration of the analyzed nitrogen series parameters for the delimited regions, according to the research methodology.</p>
Full article ">Figure 7
<p>Concentration of the analyzed phosphorous series parameters for the delimited regions, according to the research methodology.</p>
Full article ">Figure 8
<p>Concentration of the analyzed organic matter parameters for the delimited regions, according to the research methodology.</p>
Full article ">Figure 9
<p>Comparison between the pH values raised by other authors and the pH values obtained in the research [<a href="#B13-sustainability-15-15456" class="html-bibr">13</a>,<a href="#B14-sustainability-15-15456" class="html-bibr">14</a>,<a href="#B15-sustainability-15-15456" class="html-bibr">15</a>,<a href="#B16-sustainability-15-15456" class="html-bibr">16</a>,<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B18-sustainability-15-15456" class="html-bibr">18</a>,<a href="#B19-sustainability-15-15456" class="html-bibr">19</a>].</p>
Full article ">Figure 10
<p>Comparison between the values of solids raised by other authors and the values obtained in the research [<a href="#B16-sustainability-15-15456" class="html-bibr">16</a>,<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B19-sustainability-15-15456" class="html-bibr">19</a>,<a href="#B21-sustainability-15-15456" class="html-bibr">21</a>].</p>
Full article ">Figure 11
<p>Comparison between the values of ammoniacal nitrogen given by other authors and the values obtained in the research [<a href="#B16-sustainability-15-15456" class="html-bibr">16</a>,<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B19-sustainability-15-15456" class="html-bibr">19</a>,<a href="#B20-sustainability-15-15456" class="html-bibr">20</a>,<a href="#B21-sustainability-15-15456" class="html-bibr">21</a>].</p>
Full article ">Figure 12
<p>Comparison between the values of nitrate determined by other authors and the values obtained in the research [<a href="#B16-sustainability-15-15456" class="html-bibr">16</a>,<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B19-sustainability-15-15456" class="html-bibr">19</a>,<a href="#B21-sustainability-15-15456" class="html-bibr">21</a>].</p>
Full article ">Figure 13
<p>Comparison between the values of total phosphorous determined by other authors and the values obtained in the research [<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B20-sustainability-15-15456" class="html-bibr">20</a>,<a href="#B43-sustainability-15-15456" class="html-bibr">43</a>].</p>
Full article ">Figure 14
<p>Comparison between the values of COD determined by other authors and the values obtained in the research [<a href="#B15-sustainability-15-15456" class="html-bibr">15</a>,<a href="#B16-sustainability-15-15456" class="html-bibr">16</a>,<a href="#B17-sustainability-15-15456" class="html-bibr">17</a>,<a href="#B19-sustainability-15-15456" class="html-bibr">19</a>,<a href="#B20-sustainability-15-15456" class="html-bibr">20</a>,<a href="#B21-sustainability-15-15456" class="html-bibr">21</a>].</p>
Full article ">
20 pages, 2447 KiB  
Article
Treatment of Direct Red 28 Dye through Phoenix dactylifera L. Fruit Seed Biochar: Equilibrium, Kinetics, Thermodynamics, and Phytotoxicity Studies
by Riti Thapar Kapoor, Mohd Rafatullah, Husnul Azan Tajarudin, Masoom Raza Siddiqui and Mahboob Alam
Sustainability 2023, 15(21), 15266; https://doi.org/10.3390/su152115266 - 25 Oct 2023
Cited by 2 | Viewed by 1249
Abstract
Wastewater discharge into aquatic systems has become a severe threat to the ecosystem. Herein, Direct Red 28 (DR28) dye removal from an aqueous solution was executed with the application of date fruit seed biochar (DFSB). Fourier transform infrared spectra (FTIR) and scanning electron [...] Read more.
Wastewater discharge into aquatic systems has become a severe threat to the ecosystem. Herein, Direct Red 28 (DR28) dye removal from an aqueous solution was executed with the application of date fruit seed biochar (DFSB). Fourier transform infrared spectra (FTIR) and scanning electron microscopy (SEM) were utilized for the identification of functional groups and characteristics of the DFSB surface. A series of batch investigations were conducted to analyze pH, contact duration, biochar amount, dye concentration, temperature, and agitation speed on DR28 dye elimination from an aqueous medium by DFSB. The highest dye elimination, 97%, was recorded at a pH of 3 by DFSB at 250 mg/L DR28 dye concentration. The equilibrium data indicated the best fit with the Langmuir isotherm with R2 = 0.99, showing 5.83 mg/g monolayer DR28 uptake potential. The best correlation coefficient of the sorption procedure was observed with a pseudo-second-order kinetic study. Investigations on thermodynamic variables disclosed favorable, impetuous exothermic processes. The sorption process was spontaneous as well as exothermic, which was reflected by analyses of thermodynamic parameters. DFSB showed a 33% DR28 dye adsorption ability for up to five successive cycles. DFSB-treated DR28 dye solution increased seedling growth and biochemical components of pigeon pea. The results of the present investigation revealed the significant capacity of DFSB for DR28 dye elimination. Date fruit seed biochar can be applied as an environmentally benign, sustainable adsorbent for DR28 dye removal from industrial effluent, as it is available at zero cost and converts wastewater into reusable biomaterial. Thus, the application of DFSB can assist in wastewater treatment, carbon sequestration, and waste management for a sustainable future. Full article
Show Figures

Figure 1

Figure 1
<p>FTIR of DFSB (<b>a</b>) before and (<b>b</b>) after DR28 dye sorption.</p>
Full article ">Figure 2
<p>Scanning electron micrographs of DFSB adsorption procedure. (<b>a</b>) DFSB with spaces that can uptake DR28 dye and (<b>b</b>) pores with DR28 dye molecules.</p>
Full article ">Figure 2 Cont.
<p>Scanning electron micrographs of DFSB adsorption procedure. (<b>a</b>) DFSB with spaces that can uptake DR28 dye and (<b>b</b>) pores with DR28 dye molecules.</p>
Full article ">Figure 3
<p>Effect of different variables—(<b>a</b>) pH and particle size, (<b>b</b>) contact period, (<b>c</b>) concentration of dye, (<b>d</b>) DFSB amount, (<b>e</b>) agitation speed, and (<b>f</b>) temperature—on DR28 dye (250 mg/L) removal by DFSB.</p>
Full article ">Figure 4
<p>Graphical plot of point of zero charge of DFSB.</p>
Full article ">Figure 5
<p>(<b>a</b>) Langmuir, (<b>b</b>) Freundlich, (<b>c</b>) and Temkin isotherms for DR28 dye adsorption on DFSB.</p>
Full article ">Figure 6
<p>(<b>a</b>) Pseudofirst-order, (<b>b</b>) pseudo-second-order, and (<b>c</b>) Weber–Morris intraparticle diffusion models for DR28 sorption onto DFSB.</p>
Full article ">Figure 7
<p>Removal of Direct Red 28 dye by DFSB for up to five consecutive cycles.</p>
Full article ">
Back to TopTop