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Pyrolysis of SwitchgrassAmanda Drabek & Kang-Lih Chey
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IntroductionBio-Oil Components:
Bio-Oil
Switchgrass
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Goals of this Project
Design pyrolysis process to convert switchgrass to bio-oil and upgrade to liquid fuel.
Determine factors that would make process economical.
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Upgrading Options
1. Upgrade bio-oil using hydrotreating process
2. Upgrade bio-oil using catalytic deoxygenation
› Consider 5 different scenarios.
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Design Pyrolysis Process
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Lab Scale Pyrolysis Reactor System
“Bench-Scale Fluidized-Bed Pyrolysis of Switchgrass for Bio-Oil Production.” Boateng, et. al. Ind. Eng. Chem. Res. 2007.
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Industrial Scale Pyrolysis ProcessUnits = Metric Tons/hr
Switchgrass 100
Energy Required for the Pyrolysis Process: 81,812 MJ
Energy Supplied by Char: 252,000 MJ
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Selecting Reactor Type
Use fluid bed reactor.
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Optimum Reactor Temperature
Reactor Temperature is 480 °C
http://www.unh.edu/p2/biooil/bounhif.pdf
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Plant Location
Build the plant in Iowa› Centrally located in Midwest› Research currently being done in Iowa
regarding switchgrass
20 acres of land for biofuels plant› Cost of land in Iowa is $5140 per acre› Total cost of land for the plant is $102,800
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Transportation Costs
Transportation is $0.10 per ton switchgrass per mile
Plant based on 100 tons/hr switchgrass feed Transportation cost is $860 per hr
Distance Distribution
0%
10%
20%
30%
Miles 20 40 60 80 100 120 140 160 180
Distance from Biofuels Plant
% o
f Far
ms
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Upgrading Option 1: Hydrotreating
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Hydrotreating Overview
Reacts hydrogen with bio-oil to remove oxygen.
Hydrogen is produced from steam reformer.
Steam reformer uses NCG and additional methane as feed.
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Hydrotreating Economic Summary
TCI = $41.5 million
Manufacturing Cost = $157.7 million/yr
Net Profit first year = -$13.73 million
ROI = -0.33
Equipment Cost (in millions)Pyrolysis unit $1.20Hydrotreater $5.00Steam Reformer $0.69Land (acres) $0.10Total Equipment Costs $6.99
Direct CostsPurchased equipment $6.99Purchased-equipment installation $3.29Instrumentation and controls $2.52Piping $4.76Electrical systems $0.77Buildings $1.26Yard improvements $0.70Service facilities $4.89Total Direct Costs $25.17
Indirect CostsEngineering and supervision $2.31Construction expenses $2.87Legal expenses $0.28Contractor's fee $1.54Contingency $3.08Total Indirect Costs $10.07
Fixed Capital Investment $35.24Working Capital $6.22Total Capital Investment $41.47
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Break Even Points Analysis
Break even Oil Price: $119/bbl
Break even Feed Rate: 165 ton/hr
0 50 100 150 200 250 300 350
-1.5-1
-0.50
0.51
1.52
2.53
3.5
Hydrotreating Option-ROI v. Oil Price
Oil Price ($/bbl)
ROI
0 100 200 300 400 500 600
-1-0.5
00.5
11.5
22.5
33.5
Hydrotreating Option-ROI v. Feed Rate
Feed Rate (tons switchgrass/h)
ROI
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Hydrotreating: Optimized Process
Raise product price to $119/bbl Increase scale to 500 tons/hr feed
Optimized Net Profit: $200 million Optimized ROI: 4.8
Conclusion: Not significant ROI
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Conclusion from Hydrotreating Method
Not likely to be profitable.› Need to operate at a large scale because
of high capital investment.
› No significant factor that can be manipulated.
› Efficiency of process is not likely to be improved.
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Upgrading Option 2: Catalytic Deoxygenation
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Catalyst Chosen: HZSM-5 Zeolite
Produces mostly aromatic products. Produces an organic and aqueous layer
which is easily separable. Stable at high temperatures.
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Octane Numbers of Upgraded OilChemical % wt. fraction Octane #
Benzene 1.2 101Toluene 3.1 114Ethylbenzene 2.6 115.51,3-dimethylbenzene 9.4 145Propylbenzene 0.2 1271,2,4-trimethylbenzene 11.8 136Butylbenzene 0.3 97.52-methylphenol 3.3 ---1-Methyl-4-benzene 2.4 ---1,2,3,5-tetramethylbenzene 0.5 100Naphthalene 6.2 Not a component in
today’s liquid fuel.Methylnaphthalene 9.2
1-ethylnaphthalene 3.4
2,3-dimethylnaphthalene 6.3
Methylanthracene 2.6
Dimethylanthracene 0.5
Components found in today’s fuel.
High octane numbers.
Components NOT found in today’s fuel.
Niche market for Naphthalene.
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Boiling Points of Upgraded OilChemical % wt. fraction Boiling Point (oF)
Benzene 1.2 176.18Toluene 3.1 231.1Ethylbenzene 2.6 277.11,3-dimethylbenzene 9.4 358Propylbenzene 0.2 318.61,2,4-trimethylbenzene 11.8 336.9Butylbenzene 0.3 361.92-methylphenol 3.3 359.31-Methyl-4-benzene 2.4 3941,2,3,5-tetramethylbenzene 0.5 388.4Naphthalene 6.2 424.3
Methylnaphthalene 9.2 472.3
1-ethylnaphthalene 3.4 496.9
2,3-dimethylnaphthalene 6.3 511.3
Methylanthracene 2.6 646.1
Dimethylanthracene 0.5 Expected to be above the methylantracene.
Can separate components based on boiling points.
Can remove Benzene and Toluene if desired.
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Catalytic Deoxygenation ProcessUnits = Metric Tons/hr
Total Energy Produced – Total Energy Required = Energy
Remaining
252000 – 42000 = 210000 MJ
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Catalytic Deoxygenation Economics
TCI = $22.91 million
Manufacturing Cost = $121 million/yr
Net Profit first year = -$3.24 million
ROI = -0.15
Equipment Costs (in millions)Pyrolysis unit $1.20Cat Reactor $0.67regenerator $1.63storage tank $0.04separator $0.07land (acres) $0.10Total Equipment Cost $3.72
Direct CostsPurchased equipment $3.72
Purchased-equipment installation $1.75Instrumentation and controls $1.34Piping $2.53Electrical systems $0.41Buildings $0.67Yard improvements $0.37Service facilities $2.60Total Direct Costs $13.39
Indirect CostsEngineering and supervision $1.23Construction expenses $1.52Legal expenses $0.15Contractor's fee $0.82Contingency $1.64Total Indirect Costs $5.36
Fixed Capital Investment $18.75Working Capital $3.31Total Capital Investment $22.06
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Break Even Points Analysis
Break even Oil Price: $110/bbl
Break even Feed Rate: 66 tons/hr
0 100 200 300 400 500 600-2-1012345678
Catalyst Option-ROI vs. Feed Rate
Feed Rate (tons switchgrass/h)
ROI
0 50 100 150 200 250 300 350
-1.5-1
-0.50
0.51
1.52
2.53
Catalyst Option-ROI vs. Oil Price
Oil Price ($/bbl)
ROI
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Upgrade Bio-Oil using Cat. Deox.
Break even Catalyst Price: $996/ton Current Price: $1320/ton We believe that the catalyst price will
decrease when produced in bulk.
0 200 400 600 800 1000 1200 1400 1600
-0.3
-0.2
-0.1
0
0.1
0.2
0.3
0.4
0.5
0.6
Catalyst Option-ROI vs. Cata-lyst Price
Catalyst Price ($/ton)
ROI
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Alternate Scenarios
Scenario 0: original scenario Scenario 1: Decrease amount of catalyst used
from 17 g cat/g oil/min to 8.5 g cat/g oil/min Scenario 2: Regenerate catalyst 10 times
instead of 2; run on 30 minute cycles instead of hour cycles.
Scenario 3: Increase Yield of Product Oil to 23 wt %.
Scenario 4: Process is separate from refinery; add separation process and transportation costs
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Comparing Alternate Scenarios:Oil Price
Want to sell oil for cheapest price.
Scenarios 1 and 2 are best.
0 1 2 3 40
50
100
150
200
250
300
350
Breakeven Oil Price for Different Scenarios
Scenario
Oil
Pri
ce (
$/b
bl)
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Comparing Alternate Scenarios:Plant Size
Plant size is similar across all scenarios except 4.
0 1 2 3 40
10
20
30
40
50
60
70
80
Breakeven Plant Size for Different Scenarios
Scenario
Pla
nt
Siz
e (t
on
s/h
r)
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Comparing Alternate Scenarios:Catalyst Price
Want to breakeven with highest catalyst price.
Scenario 2 is best.
0 1 2 3 40
500
1000
1500
2000
2500
3000
3500
4000
Breakeven Catalyst Price for Different Scenarios
Scenario
Cat
alys
t P
rice
($/
ton
)
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Catalytic Deoxygenation: Optimized Process
Use Scenario 1 as basis Increase oil price to $110/bbl Increase scale to 500 ton/hr
Optimized Net Profit: $170 million Optimized ROI: 7.8 Conclusion: Significant ROI
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Conclusions from Scenarios
Scenarios 1 & 2 are most economical.› Scenario 1: Use less catalyst.› Scenario 2: Use catalyst for more cycles.
Optimized scenario gives reasonable ROI
Should combine process with refinery. Want to increase selectivity of catalyst.
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Components of Upgraded Bio-OilChemical % wt. fraction Octane #
Benzene 1.2 101Toluene 3.1 114Ethylbenzene 2.6 115.51,3-dimethylbenzene 9.4 145Propylbenzene 0.2 1271,2,4-trimethylbenzene 11.8 136Butylbenzene 0.3 97.52-methylphenol 3.3 ---1-Methyl-4-benzene 2.4 ---1,2,3,5-tetramethylbenzene 0.5 100Naphthalene 6.2 Not a component in
today’s liquid fuel.Methylnaphthalene 9.2
1-ethylnaphthalene 3.4
2,3-dimethylnaphthalene 6.3
Methylanthracene 2.6
Dimethylanthracene 0.5
Want to increase selectivity for blue and purple components because they are found in today’s fuel.
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Proposed Experiments
Determine how many times can you regenerate the catalyst for a set run time.
Determine minimum amount of catalyst that can give a desirable product.
Increase selectivity of catalyst for liquid product.
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Conclusions Pursue Catalytic Deoxygenation
method For catalyst:
› Decrease amount used› Increase selectivityScenario TCI
(million $)Net Profit (million $)
ROI
Hydrotreating $41.5 -$13.73 -0.33
Cat. Deox. Original
$22.06 -$3.24 -0.15
Cat. Deox. 1 $22.06 $10.09 0.46
Cat. Deox. 2 $22.06 $8.24 0.37
Cat. Deox. 3 $22.06 $10.07 0.46
Cat. Deox. 4 $22.06 -$24.32 -1.06
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Questions?
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Reactor Types
Fluidized BedCirculating Fluidized Bed Ablative