Gasifier Stoves for Bioenergy Generation from Oil Palm Residues in Humid Tropical Regions of Mexico: A Review
Abstract
1. Introduction
2. Oil Palm Expansion and Biomass Residue Generation in Mexico
2.1. Impacts of Crop Expansion on Rural Development
2.2. Territorial Transformations and Social Dynamics
2.3. Land Tenure and Crop Governance
2.4. Environmental and Socio-Ecological Impacts
2.5. Technological Innovation and Agricultural Productivity
2.6. Oil Palm, Bioenergy, and Energy Transition
2.7. Synthesis of Research Trends
3. Biomass Availability and Oil Palm Residue Generation in Mexico
Biomass Availability in Humid Tropical Regions of Mexico
4. Key Findings and Technical Limitations
4.1. Characterization and Potential of Oil Palm Residues in Mexico
4.2. Physicochemical Properties of Oil Palm Residues
| Type of Residue | Calorific Value (MJ/kg) |
|---|---|
| Empty fruit bunches (EFB) | 17.76 |
| Mesocarp fiber (MF) | 19.06 |
| Palm kernel shell (PKS) | 20.09 |
| Oil palm leaves (OPF) | 15.72 |
4.3. Classification and Applications of Oil Palm Residues
4.4. Implications for Thermochemical Conversion
5. Gasifier Stove Based on Oil Palm Residues for Cooking Applications
5.1. Fundamentals of Gasifier Stoves
5.2. Operating Principles and Stages
5.3. Types of Gasifier Stoves and Relevant Gasifier Configurations
5.4. Performance and Efficiency of Gasifier Stoves
5.5. Application of Oil Palm Residues in Gasifier Stoves
5.6. Environmental and Social Benefits
5.7. Challenges and Limitations
5.8. Integration with Energy Systems
5.9. Performance and Efficiency of Biomass Gasification Systems
6. Application of Oil Palm Residues in Gasifier Stove Systems in Mexico
6.1. Oil Palm Residues as Feedstock for Gasifier Stoves
6.2. Public Policies and Incentives for Bioenergy and Oil Palm Utilization
6.3. Integration into Decentralized Energy Systems
6.4. Ash-Related Challenges: Slagging, Fouling, and Mitigation Strategies
6.5. Tar Formation and Reduction Strategies
6.6. Gaseous and Particulate Emissions (PM, CO, and NOx)
7. Feasibility of the Proposed Approach: Socio-Economic and Environmental Aspects in Mexico
7.1. Economic Viability and Associated Costs (Collection, Transportation, and Processing)
7.2. Socio-Economic Impacts on Rural Communities
7.3. Environmental Impact and Life Cycle Assessment (LCA)
8. Opportunities for Future Research
8.1. Optimization of Small-Scale Gasification Stove Designs
8.2. Development of Low-Cost Catalysts for Tar Reduction
| Reference | Catalytic System | Tar Reduction Mechanism | Performance Metrics | Cost Considerations |
|---|---|---|---|---|
| [128] | Biochar with zinc, iron, and nickel | Metallic sites promote deoxygenation, aromatization, and syngas formation | Bio-oil yield up to 64.16%; aromatics > 50%; hydrogen 156.8 NmL g−1; iron@carbon surface area 964 m2 g−1; oxygen content < 3% | Biochar from agricultural residues; metal salts; scalable |
| [133] | Aluminum oxide in granules from sago bark ash | Increases surface area, improves interaction between fuel and gasifying agent, reducing tar | Tar reduced by 25–275%; hydrogen increased up to 31.65%; lower heating value reduced to 23.5–26.5%; H2/CO ratio 1.51–1.65 | Commercial alumina; direct addition; low cost |
| [134] | Ferric sulfate, zinc sulfate salts | Iron alters activation energies, modifies released gas profile; both enhance oxygenation | Mass loss up to 71.17%; increased CO2, H2O, CH4, CO, HCN, formic acid, acetic acid; iron more active than zinc | Simple salts; direct impregnation; very low cost |
| [135] | Dolomite, calcined dolomite (CaO/MgO) | Promotes deoxygenation, accelerates pyrolysis, reduces tar | Hydrocarbon selectivity 57.27%; liquid yield 68–73%; char 0.64%; stable over cycles; surface area up to 9.7 m2 g−1 | Natural mineral; minimal processing; highly scalable |
| [136] | Nickel nanoparticles | Promotes deoxygenation, hydrogenation, and micropore formation | Bio-oil HHV up to 42.68 MJ kg−1; biochar HHV up to 28.7 MJ kg−1; increased gas yield; improved fuel properties | Nanoparticle synthesis cost; no support required; moderate cost |
| [137] | Nickel–molybdenum/Y-NAC (hybrid zeolite/carbon) | High deoxygenation/hydrogenation, low solid residue, high cycloalkane yield | Solid yield 3.9%; deoxygenated products 50.2%; cycloalkanes 48.1%; outperforms Al2O3, ZrO2, TiO2, and CeO2 supports | Zeolite/carbon hybrid; wet impregnation; moderate cost |
8.3. Integrated Waste Management Strategies and Energy Valorization
8.4. Case Studies and Pilot Projects in Mexico
8.5. Public Policies and Incentives for Implementation
8.6. Policy Implications and Final Remarks
- Utilization of organic waste as feedstock;
- Production on marginal lands;
- Avoidance of competition with food production.
9. Conclusions
Author Contributions
Funding
Data Availability Statement
Conflicts of Interest
References
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| State | Agro-Industrial Residues | Forestry Residues | Livestock Residues | Energy Crops |
|---|---|---|---|---|
| Chiapas | Coffee pulp, sugarcane bagasse, oil palm EFB, cocoa husk. | Sawdust, wood chips, bark (from forest plantations such as teak). | Cattle manure. | Jatropha (Jatropha curcas), elephant grass. |
| Campeche | Oil palm EFB, rice husk, sugarcane bagasse, maize stover. | Forest and jungle management residues (branches, treetops). | Cattle manure. | - |
| Tabasco | Cocoa and coffee husks, banana pseudostems, citrus bagasse, oil palm residues. | - | Cattle manure (one of the highest potential sources). | Jatropha (Jatropha curcas). |
| Veracruz | Sugarcane bagasse (main residue), coffee pulp, citrus bagasse, maize and sorghum stover, pineapple residues. | Sawdust, wood chips, bark (from industrial processing). | - | - |
| Type of Waste | Applications | |
|---|---|---|
| Solid waste from palm trees | Empty Fruit Bunches (EFB): a byproduct resulting from oil extraction. | Biogas production, bioethanol production, or use as biomass for combustion. |
| Mesocarp fiber: fibrous residue obtained after oil extraction. | Solid fuel in boilers or for electricity generation. | |
| Peels (endocarp): the hard part of the fruit. Applications: | High-calorific-value biomass or raw material for activated carbon production. | |
| Liquid waste | POME (Palm Oil Mill Effluent): liquid effluent generated during the extraction process. | Biogas production (mainly methane) through anaerobic digestion. |
| Crop residues | Pruned leaves and fronds | Bioethanol production or use as biomass. |
| Trunks (derived from plantation renewal): | Energy generation or production of second-generation biofuels. |
| Reference | Stove Modelo/Type | Thermal Efficiency (%) | Test Conditions |
|---|---|---|---|
| [64] | Dual fluidized-bed gasifier, downdraft gasifier (polygeneration) | 86.6% (dual fluidized bed), 82.5% (downdraft) | Simulation, steam-to-biomass ratio = 1.5, 850 °C |
| [65] | Hydrothermal carbonization reactor (hydrochar production) | Not reported | 200 °C, 20 bar, 5–360 min |
| [66] | Fluidized-bed reactor for oxidative fast pyrolysis | Not reported | 480 °C, feed rate 15.06 kg/h |
| [67] | Microwave-assisted gasification (laboratory scale) | 19.7% (process), 55.6% (conversion) | Microwaves 250–500 W, 775 °C, 10 wt.% absorbent |
| [68] | Co-pyrolysis (fixed bed) | Not reported | 600 °C, 100 °C/s |
| [69] | Fixed-bed combustion (computational fluid dynamics) | Not reported | 8–30% moisture content, gas temperature 700 °C/400 °C |
| [70] | Ethanol stove, traditional stove | 55% (ethanol), 10% (traditional) | Regional modeling |
| [71] | Gasification, anaerobic digestion (regional) | Not reported | Gasification at 850 °C, anaerobic digestion at 56 °C |
| [72] | Integrated anaerobic digestion/gasification/solid oxide fuel cell-gas turbine/organic Rankine cycle | 54.81% (optimal), 44.93% (overall) | Simulation, high-temperature gasifier |
| [73] | Combined heat and power cycle, combined cooling, heat and power cycle (case studies) | Not reported | Not reported |
| [74] | Pyrolysis (fixed bed) | Not reported | 400–600 °C, 2 min |
| [75] | Kiln process, cookstoves | 30% (kiln), | TIMES model, India |
| [76] | Biofuel pathways | Not reported | Data envelope analysis, life cycle assessment |
| [77] | Power-to-gas, amine scrubbing | Not reported | 350–1200 °C, 5 bar |
| [78] | Pyrolysis in combined heat and power | Not reported | Not reported |
| [79] | Advanced wood gasification, combined heat and power | Not reported | Simulation, maximum 60% hydrogen in combined heat and electricity |
| [80] | Wood pelletization, bioenergy | Not reported | Not reported |
| [81] | Aqueous-phase reforming biorefinery of hydrothermal liquefaction | Not reported | 350 °C, 200 bar |
| [82] | Combined heat and power cycle (Bangladesh) | 34.6% (electric), 42% (thermal) | 35–55 °C, 20 days retention time |
| Reference | Design Parameter | Operating Range | Effect on Tar Reduction |
|---|---|---|---|
| [90] | Temperature control (auger, purge region) | 500 °C (reactor), average temperature difference 93–126 °C (auger) | Lower auger temperature reduces deposit formation (including tar); maintaining temperatures below 250–300 °C in the feeder reduces tar formation |
| [91] | Pyrolysis temperature | 550 °C (pyrolysis), 800 °C (activated carbon activation) | Activation of activated carbon at 800 °C produces an effective catalyst; high-temperature activated carbon reduces tar |
| [92] | Gasification temperature | 750–950 °C (optimum 900 °C) | Elevated temperature (above 700 °C) reduces tar through more complete conversion |
| [93] | Combustion temperature | Not reported | Not reported |
| [94] | Alkaline thermal treatment temperature | 100–600 °C (typically 500 °C) | Higher temperature combined with alkali/catalyst reduces tar via enhanced reforming |
| [95] | Gasification temperature | 700 °C, 850 °C | No mention of tar measurement was found |
| [96] | Pyrolysis temperature | 600–800 °C | High temperature and catalyst reduces bio-oil yield (tar) |
| [97] | Pyrolysis temperature | 450 °C, 550 °C, 650 °C | Higher temperature combined with catalyst increases cracking, which may reduce tar |
| Reference | Design Parameter | Evaluation Method/Remarks |
|---|---|---|
| [47] | Bluff-body (B), equivalence ratio 0.5, blended feedstock | Water Boiling Test (WBT), direct measurement. Efficiency of 13.5–17.6% |
| [110] | Throat downdraft gasifier | Calculation of gasification efficiency. Efficiency of 70% |
| [123] | Methanol boiler | Efficiency measured after conversion of 95.23% |
| [124] | Pellet composition, heating rate | Thermogravimetric analysis (TGA), reactivity index |
| [125] | Feedstock type, gasifier pressure | Process simulation |
| [126] | Entrained-flow gasification | Levelized cost, process simulation |
| [127] | Ash utilization | Carbon dioxide reduction and adsorption |
| [128] | MSW-to-aviation fuel | Life cycle assessment, greenhouse gas emissions per megajoule |
| [129] | Wood residue substitution | Avoided emissions, user surveys |
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Antonio-Zarate, M.; Rojas-Blanco, L.; Moheno-Barrueta, M.; Arellano-Cortaza, M.; Zamudio-Torres, I.; Ramirez-Morales, E. Gasifier Stoves for Bioenergy Generation from Oil Palm Residues in Humid Tropical Regions of Mexico: A Review. Biomass 2026, 6, 33. https://doi.org/10.3390/biomass6030033
Antonio-Zarate M, Rojas-Blanco L, Moheno-Barrueta M, Arellano-Cortaza M, Zamudio-Torres I, Ramirez-Morales E. Gasifier Stoves for Bioenergy Generation from Oil Palm Residues in Humid Tropical Regions of Mexico: A Review. Biomass. 2026; 6(3):33. https://doi.org/10.3390/biomass6030033
Chicago/Turabian StyleAntonio-Zarate, Marco, Lizeth Rojas-Blanco, Moises Moheno-Barrueta, Marcela Arellano-Cortaza, Ildefonso Zamudio-Torres, and Erik Ramirez-Morales. 2026. "Gasifier Stoves for Bioenergy Generation from Oil Palm Residues in Humid Tropical Regions of Mexico: A Review" Biomass 6, no. 3: 33. https://doi.org/10.3390/biomass6030033
APA StyleAntonio-Zarate, M., Rojas-Blanco, L., Moheno-Barrueta, M., Arellano-Cortaza, M., Zamudio-Torres, I., & Ramirez-Morales, E. (2026). Gasifier Stoves for Bioenergy Generation from Oil Palm Residues in Humid Tropical Regions of Mexico: A Review. Biomass, 6(3), 33. https://doi.org/10.3390/biomass6030033

