Table 2

Main research works for increasing lipid recovery from Y. lipolytica.

Y. lipolytica strain Technology Extraction process Lipid yield Advantages Disadvantages References
ATCC 20460 Conventional solvent extraction 3 g of wet yeast biomass with 10 mL chloroform:methanol (1:2, v/v); 30 min maceration, constant stirring at room temperature 6.23 ± 0.51 g/100 g of dry weight (dw) Easy to conduct
Reproducible
Easy to scale up
Limited diffusion due to strong cell walls
Lower extraction yields compared to the other treatments
(Meullemiestre et al., 2016)
Ultrasound assisted-extraction 10 g of wet biomass with 50 mL chloroform:methanol (1:2, v/v) placed in a double jacket reactor; 30 min sonication at 300 W, 20 °C 8.10 ± 0.24 g/100 g of dw Higher extraction yields compared to conventional solvent extraction Degradation of DAG into FFAs
Change in FAs profile: higher proportion of palmitic acid C16 compared to the other methods
Bead milling 3 g of wet biomass with 10 mL chloroform:methanol (1:2, v/v) placed in 20 mL tube with 20 g ceramic beads; 30 min treatment 13.16 ± 0.68 g/100 g of dw Efficient for cell disruption
Higher extraction yields compared to conventional solvent extraction
Microwave-assisted extraction 10 g of wet biomass with 50 mL chloroform:methanol (1:2, v/v) placed in a Teflon microwave reactor; 30 min treatment at 100 W, 110 °C 7.13 ± 0.45 g/100 g of dw Higher extraction yields compared to solvent extraction Degradation of DAG into FFAs
Cold drying under reduced pressure pretreatment Biomass placed in a reactor; 48 h, −80 °C, −20 mbar. Then, maceration in chloroform:methanol (1:2, v/v) 13.56 ± 0.24 g/100 g of dw Increase in processing time and energy
High emission of carbon dioxide
Freezing/defrosting pretreatment Biomass frozen for 48 h at −20 °C then placed for 12 h at 4 °C. The process is repeated 3 times followed by oil extraction in chloroform:methanol (1:2, v/v) 5.53 ± 0.43 g/100 g of dw Decrease in the use of solvents High energy consumption
High emission of carbon dioxide
Bead milling pretreatment 3 g of wet biomass with 10 mL chloroform:methanol (1:2, v/v) placed in 20 mL tube with 20 g ceramic beads; 30 min treatment, 4000 rpm. Then, oil extraction in chloroform:methanol (1:2, v/v) 12.73 ± 0.41 g/100 g of dw Decrease in the use of solvents
Low energy consumption
Microwave pretreatment 10 g of biomass placed in a Teflon microwave reactor and heated; 15 min, 45 °C, 20 W. Then, oil extraction in chloroform:methanol (1:2, v/v) 8.18 ± 0.67 g/100 g of dw Decrease in the use of solvents
JMY 5289 High pressure homogenization (HPH) pretreatment 1 kg of 15% DM cell suspension preteated with HPH (5 passes, 1500 bar). Then, oil extraction from dry biomass (after lyophilization) in n-hexane, at room temperature, 1 h, liquid/solid ratio of 10:1 (v:w), agitation 700 rpm 100% High extraction yields High energy consumption during the drying process (Drévillon et al., 2018)
1 kg of 15% DM cell suspension preteated with HPH (5 passes, 1500 bar). Then, oil extraction from wet biomass in n-hexane (ratio 1:2 (w:w)) using high-speed disperser (40 min, 1000 rpm) 79.9 ± 11.5% Low extraction yields Lower energy consumption compared to the dry route
JMY5578 Mechanical expression pretreatment 85 g yeast suspension placed in the pressing chamber; 45 min at 5.105 Pa ≈ 25 ± 0.5% Lowest extraction yields compared to the tested pretreatment techniques (Drévillon et al., 2019)
High pulsed electric field pretreatment 200 g of yeast cell suspension (15% DM) placed in treatment chamber (500 pulses, 20 Kv/cm); lyophilization; oil extraction in n-hexane (ratio 1:10, w/v), 1 h, at room temperature with agitation at 700 rpm 29.4 ± 3% Additional release of oil compared to the untreated cells
High voltage electrical discharges pretreatment 200 g of yeast cell suspension (15% DM) placed in treatment chamber (500 pulses, 2 = 40 Kv/cm); lyophilization; oil extraction in n-hexane (ratio 1:10, w/v), 1 h, room temperature with agitation at 700 rpm 31.7 ± 6.5% Additional release of oil compared to the untreated cells Degradation of the oil
Significant changes in FAs composition compared to the other treatments except for C14:0, C18:0 and C18:2
Ultrasound pretreatment 300 g yeast cells (15% DM) placed in US reactor (1 h, 400 W, 293 k); lyophilization; oil extraction in n-hexane (ratio 1:10, w/v), 1 h, room temperature with agitation at 700 rpm 35.5 ± 6.1% Increase in extraction yields compared to the untreated cells (control)
No significant change in FAs profile
HPH pretreatment Cell suspension (600 g, 15% DM) pretreated with HPH (298 K, 20 passes, 1500 × 105 Pa) 83.9 ± 4.8% Highest extraction yields compared to the tested pretreatment techniques Change in FAs profile
JMY5289 HPH and bead milling pretreatment Cell suspension (600 g, 15% DM) pretreated with HPH (25 °C, 5 passes, 1500 bar) followed by bead milling in chloroform:methanol (2:1, v:v) (stainless steel beads of 4.9 mm, and during 3 × 30 s) 99.6% Available for large scale processing
Short processing time
No change in FAs profile
(Imatoukene et al., 2020)
QU21 Liquid nitrogen with sonication Liquid nitrogen added to biomass, then sonication 10 times for 30 s each in distilled water followed by maceration in 20 mL chloroform and methanol (2:1, v:v) for oil extraction 26.5% Increase in the extraction yields compared to conventional maceration (14.3%) (Poli et al., 2013)
Po1g Sub-critical water treatment 1 g biomass dissolved in 20 mL water and treated at 175 °C for 20 min 42.69% Environmentally friendly technique
Very similar FAs profile from untreated and sub-critical water treated samples
(Tsigie et al., 2012)

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