Techno-Economic Analysis of Whole Algae Hydrothermal Liquefaction (HTL) and Upgrading System YUNHUA ZHU Susanne B. Jones, Daniel B. Anderson, Richard T. Hallen, Andrew J. Schmidt, Karl O. Albrecht, Douglas C. Elliott Pacific Northwest National Laboratory 2015 Algae Biomass Summit Washington, DC September 29 - October 2, 2015 This presentation does not contain any proprietary, confidential, or otherwise restricted information
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Techno-Economic Analysis of Whole Algae Hydrothermal Liquefaction (HTL) and
Upgrading System
YUNHUA ZHU Susanne B. Jones, Daniel B. Anderson, Richard T. Hallen, Andrew J. Schmidt,
Karl O. Albrecht, Douglas C. Elliott Pacific Northwest National Laboratory
2015 Algae Biomass Summit Washington, DC
September 29 - October 2, 2015
This presentation does not contain any proprietary, confidential, or otherwise restricted information
Growth, Harvest Dewater
20% Solids
Water & nutrient recycle
HTL Upgrading Naphtha
Diesel
CHG H2 Gen
Oil
Aqueous
Gas
NG
H2
Whole Algae HTL and Upgrading Overview
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Hydrothermal liquefaction (HTL) ~3000 psia, 350°C, no catalyst Biocrude upgrading ~ hydrotreating and hydrocracking with hydrogen in
excess of chemical consumption Catalytic Hydrothermal Gasification (CHG) ~3000 psia, 350°C, fixed
bed
Process Simulation and Cost Analysis Assumptions
Feedstock: freshwater and saltwater algae Conversion only: 1340 tons per day algae, ash free dry weight (AFDW) basis Algae delivered at 20 wt% solids (AFDW basis) $1100/ton for feedstock (AFDW basis) 40% equity financing, 10% Internal rate of return, 60% debt financed at 8% for 10 years Costs in 2011 US $ for a mature nth plant
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Feedstock Compositions: Freshwater and Saltwater Algae
CHG Capital Cost (-40% : base : +40%) HTL Capital (-40% : base : +40%)
Total Project Investment (-10% : base : +40%) Plant Scale Dry Feedstock, ton/d (2500: 1340 : 500)
No CHG - Recycle Untreated HTL Aqueous Internal Rate of Return, IRR (0% : 10% : 20%)
Fuel Yield (+10% : base : -20%) Feedstock Cost, $/AFDW ton (430: 1100 : 2000)
Cost Change from Baseline Case, $/GGE
Conclusions Algae composition and the salt in HTL aqueous phase affect the fuel yields Cultivation, harvest and dewatering (“algae feedstock cost”) cost is the largest fraction (85% to 89%) of the total production cost The HTL process cost represents the largest fraction of the conversion cost Feedstock cost and product yield are the key cost drivers
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Potential Improvements Increasing biocrude yield and reducing HTL process cost through improved HTL reaction conditions Increasing biocrude yield via improved phase separation of the HTL oil from the aqueous product Optimizing HTL aqueous phase treatment to reduce costs and enhance carbon recovery Reducing algae feedstock cost via research improvements in the cultivation, harvest and dewatering process
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Future Work in Techno-Economic Analysis
Reduce the assumed HTL/CHG throughput to more typical algal cultivation scale
Decouple the upgrading process simulation to assess a larger scale, centralized upgrader fed by multiple HTL units
Disaggregate “feedstock cost” into cultivation, harvest and dewatering costs appropriate for a given scale
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Acknowledgements
The authors would like to acknowledge funding of this work by the US Department of Energy’s Bioenergy Technologies Office (BETO)
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Additional Slides Methodology Major assumptions
Methodology
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Process model
Cost Analysis
Minimum Fuel Selling Price
(MFSP) $
gge
Conversion Yields
Operating Conditions
Whole wet algae Conversion efficiency,
Product Yields (gasoline & diesel), etc. Mass and energy