Spreadsheet: 1cdbfbcd-2cfb-463f-a5a9-e70d0e296907
Sheet: 2.  KPPs for Pyrolysis

Table 2.  Key Performance Parameters for Proposed Commercial Facility: Thermochemical- Pyrolysis Production of Biofuels
Project Title: | NREL Nov. 2010 Fast Pyrolysis to Transportation Fuels design case (NREL/TP-6A20-46586), H2 purchased Scenario
 |  |  |  |  | [Metrics projected to commercial scale, based on demonstrated data]
TECHNICAL DATA INPUTS
Section | Key Performance Parameter | Demonstrated Value(s)* | Target Value(s) (if different than demonstrated) | Basis/Justification** (consistent with Table 1) | Notes / Directions / Examples
Product (s) and By-Products | List all products (biofuels and biofuel intermediates) and by-products serving as revenue. | naphtha and diesel blendstock, fuel gas |  |  | Please list here.  Example Products: butanol, lipids, renewable diesel, jet fuel                                                               Example By-Products: electricity
Feedstock (as delivered) | Feedstock Type(s) | Corn Stover | - |  | Examples: corn stover, switchgrass, forest residues
 | Feedstock Cost ($/BDMT) | - | 83 | based on USDA data, including delivery costs
 | Feedstock Moisture (wt %) | 0.25 | - | USDA data, [NAME], 2010
 | C, H, N, O, S (wt %) (dry basis) | 47.28, 5.06, 0.8, 40.63, 0.22% | - | Adapted from USDA data, [NAME], 2010
 | Ash content wt (%) (dry basis) | 0.06 | - | USDA data, [NAME], 2010
Pyrolysis | Gas Yield (kg/BDMT) | - | 129 | based on USDA data for corn stover pyrolysis in pilot bubbling fluidized bed of quartz sand ([NAME], 2010)
 | Char/Ash Yield (kg/BDMT) | - | 164
 | Water-Phase Yield (kg/BDMT) | - | 108
 | Bio-Oil Yield (kg/BDMT) | - | 599.0000000000001
 | Bio-Oil Moisture Content (wt%) | - | not available
 | Bio-Oil Oxygen Content (wt%)  (dry basis) | - | 0.3794
 | Energy Efficiency  across Pyrolysis (%)  (LHV) | - | not available
Bio-Oil Stabilization | Catalyst(s) usage/replacement in stabilization ($/gal biofuel(s)) | - | not available |  | if applicable
(if applicable) | H2 Consumption in Stabilization (kg/gal biofuel(s)) | N/A | - |  | if applicable
 | [NAME] Yield (kg/kg of Bio-oil feed) | - | not available
 | [NAME] and Ash Reduction in Stabilization (wt%) | - | not available
 | Metals Reduction in Stabilization (wt%) | - | 0.98 | assumed guard bed performance for reduction of metals to 10 ppm levels to protect hydrotreating cats
 | [NAME] Moisture Content (wt%) | - | [same as above]
 | [NAME] (wt%) (dry basis) | - | [same as above]
Upgrading to Fuel(s)/ | Catalyst(s) usage/replacement in upgrading ($/gal biofuel(s)) | - | $1.8MM/yr catalyst replacement costs | based on typical catalyst replacement costs for petrochemical hydrotreating and hydrocracking unit operations | if applicable
[NAME]) (If applicable) | H2 Consumption in Upgrading (kg/gal biofuel(s)) | - | 0.03-0.045 | Adapted from wood pyrolysis/upgrading lab data presented publically by UOP ([NAME], J.; Nair, P.; [NAME], D.; Bain, R.; Marinangeli, R. “Converting Pyrolysis Oils to Renewable Transport Fuels: Processing Challenges & Opportunities.” National Petrochemical & Refiners Association Annual Meeting, San Diego, CA, 2008; March 9-11, 2008) | if applicable
 | Gas Yield in Upgrading (kg/gal biofuel(s) produced) | - | 0.6 (including water)
 | Liquid Fuel(s)/Product(s) Yield in Upgrading (kg/kg oil feed) | - | 0.42
 | Liquid Fuel(s)/Product(s) Oxygen Content (wt%)  (dry basis) | - | 0.015176 |  | list separately for each product stream
 | Liquid Fuel(s)/Product(s) Moisture Content (wt%) | - | not available |  | list separately for each product stream
 | Refinery Insertion Point for Liquid Fuel(s) | - | intermediate refinery insertion point (middle distillates stream) |  | if applicable, list separately for each product/steam
 | Liquid Fuel(s)/Product(s) Miscibility with Petroleum Steam(s) | - | naphtha/diesel stream miscible |  | list separately for each product stream
Overall Yields | Overall Yield from Biomass (unit/BDMT)                                                                --Jet Fuel (gal/BDMT) [NAME] (gal/BDMT) --Naphtha/gasoline (gal/BDMT)                                                                           --Export Power (kWhr/BDMT)                                                               --Export Steam (MMBTU/BDMT) --Other products/byproducts (unit/BDMT) | - | 47.8 gal/BDMT naphtha 40.8 gal/BDMT diesel 1.8 MMBTU/BDMT fuel gas | simulation based on above assumptions | Provide separately for each product and by-product (e.g. gal ethanol/BDMT), kW of excess electricity/BDMT)
 | Overall Gate-to-Gate Energy efficiency (%) (LHV) | - | 0.7 | simulation based on assumptions | ([NAME]) and by-products out)/(Biomass plus other input fuels in)
Overall Usage Rates (based on demonstrated data and projected to commercial scale) | Chemicals and Materials Costs ($/gal biofuel(s)) | - | <$0.28/gal N+D | H2 consumption and catalyst costs only; other chemical/material costs not available; based on simulations and above assumptions | Include enzymes, chemical, catalysts, import [NAME], other materials, solvents, etc
 | Utilities Imported to/Purchased for Process: --Electricity (kWhr/gal biofuel(s))                                                                   --Natural gas (MMBTU/gal biofuel(s))                                                                 --Steam (MMBTU/gal biofuel(s)) | - | 138 kWhr/BDMT power | simulation based on above assumptions | Example: purchased electricity = 1.2kWh/BDMT
 | Purchased water (gal/gal biofuel(s)) | - | not available |  | Include process water, cooling water, boiler feed water makeup, etc.
Wastes (based on demo'd data/projected to commercial) | Waste Water for Treatment (gal/gal biofuel(s)) | - | not available |  | Include assumptions for water recycle/re-use
 | [NAME] (kg/gal biofuel(s)) | - | 1.5 | simulation based on assumptions
Capital Costs***  (projected to | Commercial Plant Design Capacity (BDMT/day) | - | 2000 |  | Design capacity for capital cost estimate
commercial scale) | Total Capital Investment ($) | - | $200MM | assumed nth plant, Installed capital estimated using ICARUS, based on Aspen simulation; Indirect costs & contingency estimated using factors; Lang Factor of 5.5
Labor Costs (projected to commercial scale) | Expected Commercial Plant Staffing (FTE) | - | not available |  | Provide an estimate of the number of people it will take to operate the full-scale commercial plant. Include process operators and immediate supervision. Express as the number of Full Time Equivalent people.
* Provide the best value achieved to date based on actual data, not design specs or plans
**Describe  the basis or justification for current best result and the scale at which it was achieved. Examples of basis include: number of hours at steady state (steady state typically defined as continuous operation of the integrated process for ≥3 residence times), or the results of a number of replicate short runs of the isolated process step, etc. Include how the measurement was made (e.g. analysis of the gasifier outlet stream using gas chromatography).  Reference information in Table 1 as necessary.
***For Capital estimates, please include the level of confidence in the data and provide ranges if applicable.