Submitted:
20 May 2024
Posted:
21 May 2024
You are already at the latest version
Abstract
Keywords:
1. Introduction
2. Review Methodology
2.1. Inclusion Criteria
- Types of studies: Experimental studies, modeling studies, life cycle analyses that examine the production of biodiesel from MWS using heterogeneous solid acid catalysts.
- Types of biodiesel feedstock: Studies using primary, secondary, or digested MWS as feedstock. Studies using synthetic wastewater sludge mixtures are also eligible.
- Types of catalytic intervention: Use of heterogeneous solid acid catalysts, such as sulfated metal oxides, zeolites, heteropolyacids, and acid-modified silica, for the transesterification reaction to produce biodiesel from MWS.
- Types of outcome measures: Quantitative outcome measures like biodiesel yield, conversion rate, ester content, fuel properties, catalyst reusability and stability.
2.2. Exclusion Criteria
- Review papers, policy briefs, editorials, and other non-research articles
- Studies focused exclusively on catalyst development without application for biodiesel production
- Studies using only virgin vegetable oils, animal fats, palm or microalgae feedstock
- Studies using homogeneous acid or base catalysts
- Studies reporting insufficient data on quantitative outcome measures
- Duplicate studies or sub-studies of already included research
- Non-English studies
3. Overview of Biodiesel Production from Wastewater-Derived Sludge
3.1. Composition and Characteristics of Wastewater-Derived Sludge
3.2. Opportunities and Challenges
4. Types of Catalysts Used for Biodiesel Production
5. Heterogeneous solid acid catalysts: fundamentals and properties
5.1. Definition and Types of Solid Acid Catalysts
5.1.1. Zeolites and Zeotype Materials
5.1.2. Hetero-Polyacid (HPA)
5.1.3. Mixed Metal Oxides
5.1.4. Sulphonic Acid Group Catalysts
5.2. Advantages and Limitations of Solid Acid Catalysts
6. Application of Heterogeneous Solid Acid Catalysts in Biodiesel Production from Wastewater-Derived Sludge
6.1. Catalytic Transesterification Reaction
6.2. Mechanisms of Biodiesel Production with Solid Acid Catalysts
6.3. Effects of Catalyst Loading on Biodiesel Yield
6.4. Performance Metrics and Catalyst Evaluation
6.4.1. Catalytic Activity
6.4.2. Stability
6.4.3. Recyclability
6.4.4. Cost-Effectiveness
6.4.5. Environmental Impact
7. Synthesis and Characterization Techniques of Heterogeneous Solid Acid Catalysts
7.1. Preparation Methods
7.2. Characterization Techniques
8. Recent Advances in the Development of Heterogeneous Solid Acid Catalysts
9. Environmental and Economic Implications of Biodiesel Production Using Solid Acid Catalysts
9.1. Sustainability Assessment
9.2. Economic Viability and Techno-Economic Analysis
10. Challenges and Future Perspectives
10.1. Current Challenges and Limitations
10.2. Future Research Directions and Opportunities
11. Conclusion
Supplementary Materials
Author Contributions
Funding
Acknowledgments
Conflicts of Interest
References
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| Problem | Causative reason | Possible remedies |
|---|---|---|
| Low active sites | Using materials with low specific surface area as catalysts | Providing large interconnected pores in the catalyst |
| Limited mass transfer | Formation of various phases in the reaction mixture | Using a catalyst with a specific surface area and larger pores |
| Low reaction rate compared to others | Catalyst pore clogging and diffusion limitation on the catalyst surface | Use of appropriate co-solvents in the reaction |
| Inactivation in the reaction medium | The presence of impurities in the raw material | Synthesis of catalyst with high water adsorption capability |
| High reaction temperature required | Blocking of the active sites of the catalyst due to water present in the reaction mixture | Catalyst with high water adsorption capability, using a catalyst with a specific surface area and larger pores |
| Need for high catalyst loading | Water adsorption on the surface of the catalyst | Synthesis of catalyst with high water adsorption capability |
| Removal of functional groups due to leaching | Ionic groups hydrolyzed by water | Use an appropriate catalyst preparation technique. |
| Authors | Year | Catalyst | Catalytic activity biodiesel yield (%B.Y.) OR FAME yield (%FAME) |
Optimal condition | Recyclability | Cost-effectiveness | Environmental Impact | Ref. |
|---|---|---|---|---|---|---|---|---|
| Hatami et al. | 2023 | SBGAC-PhSO3Ha | 17.34% B.Y. | Reaction time of 14 h, reaction temperature of 70 °C, methanol-to-lipid relative content of 40 mL/g, and catalyst loading of 20 wt %. | Density decreased by 62.6% after the fifth reaction cycle | N.M. | N.M. | [75] |
| Siddiquee et al. | 2011 | as-synthesized SBA-15 | 30.14% B.Y. | Temperature of 135 °C and a pressure of 135 psi for 3 h reaction time | N.M. | N.M. | N.M. | [59] |
| Melero et al. | 2015 | Zr-SBA-15 | 15.5% FAME | 209 °C, 2000 rpm, 50:1 methanol to saponifiable matter molar ratio, 12.5 wt% catalyst based on lipids mass | N.M. | N.M. | N.M. | [76] |
| Sangaletti-Gerhard | 2015 | Sulfuric acid | 36% FAME | Temperature of 55 °C, 7 h reaction time, methanol-to- sludge ratio of 20 mL/g | N.M. | 11.27 US$ /kgFAME | N.M. | [77] |
| Novozym435 | 52% FAME | Temperature of 55 °C, 7 h reaction time, methanol-to- sludge ratio of 20 mL/g | For 5 times reaches an energy efficiency of 66%, while after 17 times reused 100% energy efficiency | 1143.14 US$ /kgFAME | low | |||
| Booramurthy et al. | 2022 | Fe3O4/BaO | 97.6% B.Y. | 18:1 molar ratio of methanol/oil, 8 wt% of catalyst loading, Temperature of 65 °C, 5 h reaction time, | There was not reduction in yield of biodiesel until the seventh cycle and 86 wt% recovery of catalyst was recovered | N.M. | N.M. | [78] |
| Zhang et al. | 2020 | SO4/Al2O3-SnO2 | 73.3% B.Y. | 0.8 g catalyst loading, Temperature of 130 °C, 4 h reaction time, | N.M. | N.M. | N.M. | [79] |
| Saravanan et al. | 2022 | Ca/Fe3O4/Cs2O | 98.6% FAME | 20:1 molar ratio of methanol/oil, 9 wt % of catalyst loading, Temperature of 65 °C, 5 h reaction time, | up to five cycles, the yield of biodiesel was above 90 wt % | N.M. | N.M. | [80] |
| Nabgan et al. | 2022 | 3CaO–TiO2 | 97.2% B.Y. | 20:1 molar ratio of methanol/oil, 9 wt % of catalyst loading, Temperature of 70 °C, 2 h reaction time, | up to five runs with negligible activity loss | N.M. | environmentally friendly | [71] |
| Patino et al. | 2021 | Amberlyst IR120 | 32.9% FAME | 33:1 MeOH/sludge ratio, 1:2 catalyst/sludge ratio, Temperature of 120 °C, 21 h reaction time, | six times with negligible catalytic activity loss | N.M. | N.M. | [81] |
| Hashmi et al. | 2022 | Amberlyst A21 | 95.52% B.Y. | 20:1 molar ratio of FFAs to ethanol, acidic resin weight of 6%, Temperature of 70 °C, 8 h reaction time, | N.M. | annual net profit gain of Pakistani rupees Rs 54.89 and Rs 93.32 million | N.M. | [82] |
| I. Ngoie et al. | 2019 | CMSG/ZVINPs, | 88% B.Y. | 6:1 molar ratio of methanol/oil, catalyst dosages of 8 wt.% , Temperature of 75 °C, 2 h reaction time, | 27% decrease in biodiesel yield after four reaction cycles | N.M. | N.M. | [83] |
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