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微藻生質能源技術微藻生質能源技術微藻生質能源技術微藻生質能源技術−−−− Micro-Algal Bioenergy Technology
林昀輝林昀輝林昀輝林昀輝
工業技術研究院工業技術研究院工業技術研究院工業技術研究院 能源與環境研究所能源與環境研究所能源與環境研究所能源與環境研究所
2010.04.24
2010生質能源技術推廣研討會
2Copyright 2008 ITRI 工業技術研究院
Outline
• Biodiesel in Taiwan• Advantages of Micro-algal Biofuel • Commercialization Challenges• Micro-algae Research at ITRI • Concluding Remarks
2
3Copyright 2008 ITRI 工業技術研究院
Biodiesel in Taiwan
2006 20082007 2009 2010
0.65 6.50
45
100
Biodiesel Target (1,000 kL)
50
Mandatory B2 - 2010.01
Mandatory B1 - 2008.07~ 2009.12
Green County Demo Program2007.07~ 2008.06- B1 in the two demo counties
Biodiesel Fleet Program2006.10~ 2008.06- Public transportation buses fueled by B2 in two cities
Biodiesel 2010: B2 � Current feedstock:Waste cooking oil
� Sustainable feedstock
� Non-food
� Environmental and ecological friendly
� Energy effectiveness
� Cost Competitive
4Copyright 2008 ITRI 工業技術研究院
Advantages of Micro-algal Biofuel
• Effective carbon capture– Can utilize waste CO2 streams– Capture efficiency between 50~80%
in photobioreactors
– 183 ton-CO2 / 100 ton-biomass
• Higher yields than terrestrial plants– Higher oil content, growth rate and
cell density
• Non-food feedstock• Potential for cascade
production– oils, protein, and carbohydrates
Ref: (1) M.E. Huntley and D.G. Redalje, Mitigation and Adaptation Strategies for Global Change 12, (2007) 573–608(2) P. M. Schenk et al., Bioenerg. Res., (2008)(3) Y. Chisti / Biotechnology Advances 25 (2007) 294–306(4) NREL, A Look Back at the U.S. Department of Energy’s Aquatic Species Program: Biodiesel from Algae (1998)
Potential Algal Oil Yields
*Replacing 5% of diesel consumption in Taiwan requires ~3,000 hectares
93,500 Algae (50 g/m2/day at 50% lipid)*
11,000 Algae (10 g/m2/day at 30% lipid)
5,900 Oil palm
1,900 Jatropha
1,200 Rapeseed/Canola
950 Sunflower
570 Mustard seed
450 Soybean
Oil yield
Liters/hectare-yrCrops
93,500 Algae (50 g/m2/day at 50% lipid)*
11,000 Algae (10 g/m2/day at 30% lipid)
5,900 Oil palm
1,900 Jatropha
1,200 Rapeseed/Canola
950 Sunflower
570 Mustard seed
450 Soybean
Oil yield
Liters/hectare-yrCrops
3
5Copyright 2008 ITRI 工業技術研究院
Land-use Efficiency
Adapted from: 2009_USDOE_National Algal Biofuels Technology Roadmap
The area needed to produce a sufficient amount of biomass to produce liquid fuel to displace all gasoline used in the USA (2006)
Adapted from: Current Opinion in Biotechnology 2008
The amount of land required to replace 50% of the current petroleum distillate consumption using soybean (gray) and algae (green).
6Copyright 2008 ITRI 工業技術研究院
Suitable Area for Algae Growth
•Suitable land for algae farms +/- 37 o of equator•Temperature limit of > 15 ℃ annual average
4
7Copyright 2008 ITRI 工業技術研究院
Biofuel from Micro-Algae
Biomass Harvesting
Processing
Biofuels����biodiesel ����biogas����ethanol ����jet fuel
Reclaimed Water����nutrient recycling
Co-products����feeds����fertilizers����glycerin����others
Waste CO2 & Heat����Power generation����Industrial processing����Wastewater treatment
Impaired Water����Sea water����Brackish water����Wastewater
Sunlight/CO 2(photoautotrophic)
Organic Carbon(heterotrophic)
O2
Algae Production SystemPonds, PBR’s, Hybrid Systems
CO2
8Copyright 2008 ITRI 工業技術研究院
Production of Algae Oil
PhotobioreactorTemp controlLight distribution & intensity controlPredator control
Makeup water CO2 availabilityNutrient supplyStarting species
Growth rateOil content & FA profileResistance to invasion
AlgaeCultivation
LipidRecovery
BiodieselProduction
De-watering methodsLipid extractionPurificationCosts, energy inputEnvironmental issuesValue from residual
biomass
Fatty acid profilesCosts and LCAFuel
characteristicsEnergy densityCarbon numbersCloud pointStabilityConsistency
5
9Copyright 2008 ITRI 工業技術研究院
Cost Target
1 ha10.62€/kg
100 ha4.02€/kg
Target0.4€/kg
Table adapted from: Biofuel from microalgae (Rene H. Wijffels)
The lack of any mass/commercial production of algal oil means its cost is unknown and high
10Copyright 2008 ITRI 工業技術研究院
Challenges
� Continuous cultivation of highly productive oleaginous micro algae in large scale field
• Algal strain selection and improvement
• Photobioreactor• Sources of CO 2 and nutrients• Cost and reliability
� Low cost down stream processing
• Harvest• Drying• Extraction• Water recycling• Energy consumption
� Co-productsTime
Cost
ScaleScal
e-up
and
Cost
Redu
ctio
n
~US$5/kg-biomass
~US$5/kg-biomass
US$0.25/kg?US$0.25/kg?
6
11Copyright 2008 ITRI 工業技術研究院
Current Status of Micro-Algae Biofuel Technology
• NREL’s Aquatic Species Program (1978-1996)– 3,000 strains collected and
screened – 1,000 m2 outdoor test facility:10
g/m2/day biomass overall, 50 g/m2/day peak
– Est. algal oil cost ranges from $61 to $127 per barrel
• Industry moves into demonstration system– Shell, Chevron…– BP?– Others
Ref:National Geographic, 2007.10
GreenFuel Technologies’ photobioreactor system was temporarily shut down in July, 2007 due to increasing cost and technical problems
Photobioreactor in Klötze, Germany; the 700 m3 are distributed in 500 km of tubes and produce up to 100 t algae biomass per year (www.algomed.de)
12Copyright 2008 ITRI 工業技術研究院
Development of Photo-bioreactors
GreenFuel’s 3D Matrix Algae Growth Engineering Scale Unit, “triangle airlift reactor”
Solar Bioreactor (Utah-State University)
Solix Biofuel Inc.(U.S.A)AlgaeLink (Holland)
The worlds largest closed photo-bioreactor in Klötze, near Wolfsburg, Germany
A 1000 L helical tubular photo-bioreactor at Murdoch University, Australia.
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13Copyright 2008 ITRI 工業技術研究院
Research at ITRI−−−−Isolation of Indigenous Microalgae
Cooperated with Prof. Jane-Yii Wu, Department and Graduate Program of BioIndustry Technology, DaYeh University
14Copyright 2008 ITRI 工業技術研究院
Research at ITRI −−−− Algae Cultivation
0 2 4 6 8 10 120.0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
Bio
mas
s (g
/L)
Time (days)
■: Chlorella sp. ●: Chlorella minutissima ▲: Dunaliella salina▼: Dunaliella primolecta □: Isochrysis aff. Galbana ○: Nannochloropsis oculata
�: Tetraselmis sp. △: Tetraselmis suecica ▽: Tetraselmis chuii
ConditionWorking Volume: 5 L f/2 mediumTemperature: 25 ±±±± 1 oCLight intensity ~220 µµµµEm-2s-1
• 3 strains of Tetraselmis have higher biomass concentration( 0.51-0.63 g/L), but lower lipid content.
• One liter of sample was withdrew for lipid content and fatty acid composition analysis
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15Copyright 2008 ITRI 工業技術研究院
Research at ITRI −−−− Lipid Content
Chlore
lla sp
.
Chlore
lla m
inutis
sima
Dunali
ella pr
imole
cta
Dunali
ella sa
lina
Isoch
rysis
aff. g
alban
a
Nanno
chlor
opsis
ocula
ta
Tetras
elmis
chuii
Tetras
elmis
sp.
Tetrase
lmis
suecic
a
Lipid extracted by MeOH/CHCl3 = 1/2(v/v)
0
10
20
30
40
50
60
Lipi
d C
onte
nt (
%)
3 days 6 days 9 days 12 days
• The crude lipid content can be as high as 50%
•
ConditionFrozen cell was extracted by chloroform/MeOH = 2/1Lipid content was calculated as: %100×
celldriedofWeighr
lipidcrudeofWeight
16Copyright 2008 ITRI 工業技術研究院
Research at ITRI−−−− Composition of Fatty Acid
Procedure
Isochrysis aff. galbana
Chlorella minutissimaLipid (from microalgae)
Saponification
Esterification
GC Analysis
C14:0
C14:0
C16:0
C16:0
C16:1
EPA
DHA
C18:1
C18:1
(Method: CNS 15051)
C18:3
C18:2
C16:1
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17Copyright 2008 ITRI 工業技術研究院
Research at ITRI−−−− Composition of Fatty Acid
Fatty Acid Composition (%)
UnknownDHAEPAC18:3C18:2C18:1C18:0C16:1C16:0C14:0
37.8 ND4.5 13.4 6.5 12.5 1.0 0.4 22.8 1.1 Tetraselmis suecica
43.2 ND4.8 15.7 6.7 8.3 0.6 0.4 18.9 1.3 Tetraselmis sp.
38.9 ND3.4 15.6 7.9 7.9 0.5 1.1 23.7 1.0 Tetraselmis chuii
7.7 ND9.3 ND1.1 10.9 1.6 26.1 38.4 4.9 Nannochloropsisoculata
29.2 12.2 0.5 5.5 2.0 15.8 0.6 4.5 13.7 16.3 Isochrysis aff.galbana
26.4 NDND19.1 9.7 15.4 2.0 0.6 26.0 0.8 Dunaliella salina
33.7 NDND27.7 3.7 6.7 1.2 0.6 25.7 0.7 Dunaliellaprimolecta
6.6 ND9.0 ND1.4 7.9 1.7 28.3 37.5 7.6 Chlorella minutissima
27.5 NDND11.6 13.3 13.6 2.2 1.4 29.5 1.1 Chlorella sp.
* Sampled from 12th-day cultivation
18Copyright 2008 ITRI 工業技術研究院
Research at ITRI−−−− Comparisons of Outdoor and Indoor
Cultivation• Working volume was 5 L
• Half of the culture was harvested when the OD was reach 2
• Temperature difference can be as high as 20 oC(from 25 to 45oC)
• 3 strains can be survived• The growth rate of
outdoor cultivation was 3/4 of those in indoor cultivation
0 10 20 30 400.5
1.0
1.5
2.0
2.5
Tem
p (O
C)
pH
Cel
l con
c. (
OD
)
time (day)
891011
20
30
40
50
45 oC
25 oC
Red::::OutdoorBlack::::Indoor (temp was controlled between25-30 oC)
Nannochloropsis oculata
10
19Copyright 2008 ITRI 工業技術研究院
Research at ITRI −−−− Composition of the Extract
Oil layerH2O layer
Lipid = Triglyceride ?
Triglycerides were converted to its FAME and analysis by GC
10.0 32.6 18.5 Total Extract (wt%)
5.48.79.8Total Triglyceride Extracted (wt%)
53.7 26.5 53.0FAME Content in Extract (wt%)
SC-CO2Folch methodSoxhlet MethdMethod
20Copyright 2008 ITRI 工業技術研究院
Research at ITRI −−−− Comparison of Triglyceride/FFA Extraction
5.4 wt%Undisrupted algae cell (H2O: 0 wt%)
SC-CO2
12.2 wt%Disrupted algal cell (H2O: 82.4 wt%)
SC-CO2+MEOH
15.7 wt%Disrupted algae cell (H2O: 0 wt%)
SC-CO2
11.3 wt%Disrupted algal cell(Water content 79.2%)
Solvent method
8.7 wt%Undisrupted algae cell (H2O: 0 wt%)
Folch method
9.8 wt%Undisrupted algae cell (H2O: 0 wt%)
Soxhlet Methd
3.4 wt%Undisrupted algae cell (H2O: 68.0 wt%)
SC-CO2
FAMESampleMethods
11
21Copyright 2008 ITRI 工業技術研究院
Research at ITRI −−−− Downstream Process Optimization
Cultivation
�Open Ponds
�Closed Systems
- Photobioreactor
-Vertical Systems (Hanging bag)
Conditioning
�Stressing
Concentration�Centrifuge�Filter Press
Harvesting�Filtration�Flocculation�Gravity Settling
Extraction�Mechanical
- Extruder -High Pressure Homogenizer-Bead Mill- Expeller Press- Steam Explosion
�Chemical- Solvent Extraction- Supercritical Fluid Extraction- Microwave Extraction- Ultrasonic Extraction- Supersonic Extraction
Drying
�No Drying
�Ambient Air
�Heated
1-3 g Biomass/L10-20% lipids
80-90% DM20-40% lipids
95% recovery95% lipids
60-80% DM20-40% lipids
1-3 g Biomass/L20-40% lipids 5-100 g Biomass/L
20-40% lipids
Solvent Revoery
�Distillation (if using solvent)
Biodiesel Production
�Aspen Plus (Process Simulation)�Aspen Process Economic Anlyzer
Downstream Process
Upstream ProcessCultivation
�Open Ponds
�Closed Systems
- Photobioreactor
-Vertical Systems (Hanging bag)
Conditioning
�Stressing
Concentration�Centrifuge�Filter Press
Harvesting�Filtration�Flocculation�Gravity Settling
Extraction�Mechanical
- Extruder -High Pressure Homogenizer-Bead Mill- Expeller Press- Steam Explosion
�Chemical- Solvent Extraction- Supercritical Fluid Extraction- Microwave Extraction- Ultrasonic Extraction- Supersonic Extraction
Drying
�No Drying
�Ambient Air
�Heated
1-3 g Biomass/L10-20% lipids
80-90% DM20-40% lipids
95% recovery95% lipids
60-80% DM20-40% lipids
1-3 g Biomass/L20-40% lipids 5-100 g Biomass/L
20-40% lipids
Solvent Revoery
�Distillation (if using solvent)
Biodiesel Production
Cultivation
�Open Ponds
�Closed Systems
- Photobioreactor
-Vertical Systems (Hanging bag)
Conditioning
�Stressing
Concentration�Centrifuge�Filter Press
Harvesting�Filtration�Flocculation�Gravity Settling
Extraction�Mechanical
- Extruder -High Pressure Homogenizer-Bead Mill- Expeller Press- Steam Explosion
�Chemical- Solvent Extraction- Supercritical Fluid Extraction- Microwave Extraction- Ultrasonic Extraction- Supersonic Extraction
Drying
�No Drying
�Ambient Air
�Heated
1-3 g Biomass/L10-20% lipids
80-90% DM20-40% lipids
95% recovery95% lipids
60-80% DM20-40% lipids
1-3 g Biomass/L20-40% lipids 5-100 g Biomass/L
20-40% lipids
Solvent Revoery
�Distillation (if using solvent)
Biodiesel Production
�Aspen Plus (Process Simulation)�Aspen Process Economic Anlyzer
Downstream Process
Upstream Process
Focus on the advanced technologies for Harvest, cel l disruption and extraction of oil and high value che micals
22Copyright 2008 ITRI 工業技術研究院
0
10
20
30
Ene
rgy
Con
sum
ptio
n (k
W-h
/ kg-
oil)
Energy Consumption-Downstream Process
Reduce the use of L- CO2
Aspen Plus (exp. data and literatures)
Lardon(2009)
70
1
Hexane
90% (w/w)
90
100
L-CO2/SC-CO2
15 % (w/w)
959098Extraction yield(%)
300185Solvent (g)/Biomass (g)
L-CO2/SC-CO2
Hexane/MeOHHexaneSolvent
15 % (w/w)15 % (w/w)95% (w/w)Biomass Conc. before extraction
■:Extraction■:Cell disruption■:Drying ■:Culture/Harvest
Energy content ofBiomass for 1 kg oil
Ref: Life-Cycle Assessment of Biodiesel Production from Microalgae, Lardon et. al. (2009)
12
23Copyright 2008 ITRI 工業技術研究院
Concluding Remarks
• Micro-algae has great potential as biofuel feedstoc k
• To make the process economically viable is more challenge in Taiwan than other areas due to the higher costs of land and labor and more precious water resource
• ITRI will focus on the development of key technologies and collaborate with all sources of relevant government agencies, research organizations, academia, and private sector
24Copyright 2008 ITRI 工業技術研究院
Financial support provided by the Bureau of Energy, MOEA, R.O.C. is acknowledged.
Thank you for your attention.
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