Selected examples of comparative AOP in the treatment of olive mill wastewater
| References . | Technique . | OMW source . | Initial pollutant concentration . | Removal efficiency . | Operation conditions . | Mode . | Specific energy consumed . | Operating cost . |
|---|---|---|---|---|---|---|---|---|
| Canizares et al. (2009) | Fe2+/Fe3+/H2O2 | Not identified | Not identified | %COD = 73.98% %TOC = 70.72% | pH = 3 ± 0.1 V = 100 mL [Fe2+] = 700 mg/L [H2O2] = 18,000 mg/L | Batch | – | 0.7–3.0 €/kg equivalent O2 |
| Mert et al. (2010) | Fe2+/H2O2 Fe3+/H2O2 | Not identified | COD = 115,000 mg/L TPh = 5,580 mg/L | Fe2+/H2O2 %COD = 90% %TPh = 91% Fe3+/H2O2 %COD = 93% %TPh = 95% | pH = 3 [Fe2+] = 3,000 mg/L [H2O2] = 3,500 mg/L [Fe3+] = 2,500 mg/L [H2O2] = 3,000 mg/L | Batch | – | 4.81 €/kg equivalent O2 4.29€/kg equivalent O2 |
| Canizares et al. (2009) | O3/H2O2 | Not identified | Not identified | %COD = 77.2% %TOC = 67.8% | V = 2 L Flow-rate: 0.5 L/min | Batch | 1,814 kWh/m3 | 8.5–10.0 €/kg equivalent O2 |
| Michael et al. (2014) | H2O2/Fe2+ (Fe3+)/UV | Three-phase | COD = 13,000 mg/L | %COD = 87% | [Fe2+] = 80 mg/L [H2O2] = 1000 mg/L Irradiation time = 4 h | Batch | – | 0.16 € /kg COD removed |
| Ahmed et al. (2011) | H2O2/Fe2+ (Fe3+)/UV | Three-phase | COD = 2000–7000 mg/L TOC = 180–300 mg/L | %COD = 95% | pH = 3 [Fe2+] = 30 mg/L [H2O2] = 3000 mg/L Temperature = 26 °C Irradiation time = 3 h | Batch | 3.15 € /m3 | |
| YalılıKılıç et al. (2013) | Acide cracking + coagulation + ultrafiltration + O3/H2O2/UV | Not identified | COD = 128,000 mg/L TPh = 3440 mg/L TOC = 26,400 mg/L | %COD = 99.44% %TPh = 99.93% %TOC = 99.40% | pH = 3 Temperature = 20 °C CH2O2 = 500 mg/L [H2O2] = 700 mg/L | Batch | – | 7.15 € /m3 |
| Chatzisymeon et al. (2009c) | TiO2/UV | Three-phase | COD = 5100 mg/L | %COD = 20% | pH = 4.8 Temperature = 28 ± 2 °C V = 350 mL Treatment times = 4 h | Batch | 5,000 kWh/kg COD removed | – |
| Canizares et al. (2009) | CDEO | Not identified | Not identified | %COD = 98.37% %TOC = 99% | V = 0.6 L | Batch | 110 kWh/m3 | 2.4–4.0 €/kg equivalent O2 |
| Chatzisymeon et al. (2009b) | BDD anodic | Three-phase | COD = 40,000 mg/L TPh = 3500 mg/L | %COD = 19% %PP = 36% | Treatment time = 15 h Current intensity = 20 A [H2O2] = 500 mg/L | Batch | 96 kWh/kg COD removed | 7–10 €/kg COD removed |
| Hanafi et al. (2010) | Electrocoagulation | Classic process | COD = 20,000 mg/L PP = 260 mg/L | %COD = 70% %PP = 70% | Aluminum electrode Treatment time = 15 min Current density = 250 A/cm3 | Batch | 2.63 kWh/kg COD removed | 0.27 € /kg COD removed |
| Israilides et al. (1997) | Electroxidation | Not identified | COD = 178,220 mg/L TOC = 26,550 mg/L VSS = 46,620 mg/L TPh = 11,410 mg/L | %COD = 93% %TOC = 80.4% %VSS = 98.7% %TPh = 99.4% | Ti/Pt electrode Treatment time = 10 h Current density = 0.26 A/cm2 | Batch | 12.3 kWh/kg COD removed | – |
| Un et al. (2008) | Electroxidation | Three-phase | COD = 41,000 mg/L PP = 215 mg/L Turbidity = 4,050 NTU Oil-grease = 1970 mg/L | %COD = 99.6% %PP = 100% Turbidity = 99.54% Oil-grease = 99.54% | Ti/RuO2 anode Treatment time = 7 h Temperature = 40 °C Current density = 35 mA/cm2 Recirculation rate = 7.9 mL/s | Batch | 5.35–27.02 kWh/kg COD | 0.88 €/kg COD removed |
| Amaral-Silva et al. (2017) | Fenton-coagulation-biological | Not identified | COD = 6450 mg/L TSS = 3190 mg/L TPh = 21 mg/L | % COD = 38% %TSS = 40% % COD = 89% % COD = 43% % COD = 62% % COD = 95% | Lab scale Coagulation: pH = 3.4 [Fe2(SO4)3] = 3000 mg/L Fenton: [Fe2+] = 1500 mg/L [H2O2] = 15,000 mg/L Industrial scale Flow rate: 1.5 m3/h V = 450 m3 T = 22 ± 2 Coagulation: pH = 3.2–3.8 [Fe2(SO4)3] = 2500– 3000 mg/L Fenton: Biological Treatment time: 60 days | Batch Continuous | 2.96 kWh/m3 | 1.44 €/kg COD removed 2.7 €/m3 |
| References . | Technique . | OMW source . | Initial pollutant concentration . | Removal efficiency . | Operation conditions . | Mode . | Specific energy consumed . | Operating cost . |
|---|---|---|---|---|---|---|---|---|
| Canizares et al. (2009) | Fe2+/Fe3+/H2O2 | Not identified | Not identified | %COD = 73.98% %TOC = 70.72% | pH = 3 ± 0.1 V = 100 mL [Fe2+] = 700 mg/L [H2O2] = 18,000 mg/L | Batch | – | 0.7–3.0 €/kg equivalent O2 |
| Mert et al. (2010) | Fe2+/H2O2 Fe3+/H2O2 | Not identified | COD = 115,000 mg/L TPh = 5,580 mg/L | Fe2+/H2O2 %COD = 90% %TPh = 91% Fe3+/H2O2 %COD = 93% %TPh = 95% | pH = 3 [Fe2+] = 3,000 mg/L [H2O2] = 3,500 mg/L [Fe3+] = 2,500 mg/L [H2O2] = 3,000 mg/L | Batch | – | 4.81 €/kg equivalent O2 4.29€/kg equivalent O2 |
| Canizares et al. (2009) | O3/H2O2 | Not identified | Not identified | %COD = 77.2% %TOC = 67.8% | V = 2 L Flow-rate: 0.5 L/min | Batch | 1,814 kWh/m3 | 8.5–10.0 €/kg equivalent O2 |
| Michael et al. (2014) | H2O2/Fe2+ (Fe3+)/UV | Three-phase | COD = 13,000 mg/L | %COD = 87% | [Fe2+] = 80 mg/L [H2O2] = 1000 mg/L Irradiation time = 4 h | Batch | – | 0.16 € /kg COD removed |
| Ahmed et al. (2011) | H2O2/Fe2+ (Fe3+)/UV | Three-phase | COD = 2000–7000 mg/L TOC = 180–300 mg/L | %COD = 95% | pH = 3 [Fe2+] = 30 mg/L [H2O2] = 3000 mg/L Temperature = 26 °C Irradiation time = 3 h | Batch | 3.15 € /m3 | |
| YalılıKılıç et al. (2013) | Acide cracking + coagulation + ultrafiltration + O3/H2O2/UV | Not identified | COD = 128,000 mg/L TPh = 3440 mg/L TOC = 26,400 mg/L | %COD = 99.44% %TPh = 99.93% %TOC = 99.40% | pH = 3 Temperature = 20 °C CH2O2 = 500 mg/L [H2O2] = 700 mg/L | Batch | – | 7.15 € /m3 |
| Chatzisymeon et al. (2009c) | TiO2/UV | Three-phase | COD = 5100 mg/L | %COD = 20% | pH = 4.8 Temperature = 28 ± 2 °C V = 350 mL Treatment times = 4 h | Batch | 5,000 kWh/kg COD removed | – |
| Canizares et al. (2009) | CDEO | Not identified | Not identified | %COD = 98.37% %TOC = 99% | V = 0.6 L | Batch | 110 kWh/m3 | 2.4–4.0 €/kg equivalent O2 |
| Chatzisymeon et al. (2009b) | BDD anodic | Three-phase | COD = 40,000 mg/L TPh = 3500 mg/L | %COD = 19% %PP = 36% | Treatment time = 15 h Current intensity = 20 A [H2O2] = 500 mg/L | Batch | 96 kWh/kg COD removed | 7–10 €/kg COD removed |
| Hanafi et al. (2010) | Electrocoagulation | Classic process | COD = 20,000 mg/L PP = 260 mg/L | %COD = 70% %PP = 70% | Aluminum electrode Treatment time = 15 min Current density = 250 A/cm3 | Batch | 2.63 kWh/kg COD removed | 0.27 € /kg COD removed |
| Israilides et al. (1997) | Electroxidation | Not identified | COD = 178,220 mg/L TOC = 26,550 mg/L VSS = 46,620 mg/L TPh = 11,410 mg/L | %COD = 93% %TOC = 80.4% %VSS = 98.7% %TPh = 99.4% | Ti/Pt electrode Treatment time = 10 h Current density = 0.26 A/cm2 | Batch | 12.3 kWh/kg COD removed | – |
| Un et al. (2008) | Electroxidation | Three-phase | COD = 41,000 mg/L PP = 215 mg/L Turbidity = 4,050 NTU Oil-grease = 1970 mg/L | %COD = 99.6% %PP = 100% Turbidity = 99.54% Oil-grease = 99.54% | Ti/RuO2 anode Treatment time = 7 h Temperature = 40 °C Current density = 35 mA/cm2 Recirculation rate = 7.9 mL/s | Batch | 5.35–27.02 kWh/kg COD | 0.88 €/kg COD removed |
| Amaral-Silva et al. (2017) | Fenton-coagulation-biological | Not identified | COD = 6450 mg/L TSS = 3190 mg/L TPh = 21 mg/L | % COD = 38% %TSS = 40% % COD = 89% % COD = 43% % COD = 62% % COD = 95% | Lab scale Coagulation: pH = 3.4 [Fe2(SO4)3] = 3000 mg/L Fenton: [Fe2+] = 1500 mg/L [H2O2] = 15,000 mg/L Industrial scale Flow rate: 1.5 m3/h V = 450 m3 T = 22 ± 2 Coagulation: pH = 3.2–3.8 [Fe2(SO4)3] = 2500– 3000 mg/L Fenton: Biological Treatment time: 60 days | Batch Continuous | 2.96 kWh/m3 | 1.44 €/kg COD removed 2.7 €/m3 |