119/1/2006

Biomass Gasification

Presented byDr. Richard L. Bain, Principal Research Supervisor, Biorefinery AnalysisBiorefinery Analysis and Exploratory Research GroupNational Bioenergy Center

USDA Thermochemical Conversion WorkshopPacific Northwest National LaboratoryRichland, WASep 6, 2006

9/1/2006 2

Disclaimer and Government License

This work has been authored by Midwest Research Institute (MRI) under Contract No. DE-AC36-99GO10337 with the U.S. Department of Energy (the “DOE”). The United States Government (the “Government”) retains and the publisher, by accepting the work for publication, acknowledges that the Government retains a non-exclusive, paid-up, irrevocable, worldwide license to publish or reproduce the published form of this work, or allow others to do so, for Government purposes.

Neither MRI, the DOE, the Government, nor any other agency thereof, nor any of their employees, makes any warranty, express or implied, or assumes any liability or responsibility for the accuracy, completeness, or usefulness of any information, apparatus, product, or process disclosed, or represents that its use would not infringe any privately owned rights. Reference herein to any specific commercial product, process, or service by trade name, trademark, manufacturer, or otherwise does not constitute or imply its endorsement, recommendation, or favoring by the Government or any agency thereof. The views and opinions of the authors and/or presenters expressed herein do not necessarily state or reflect those of MRI, the DOE, the Government, or any agency thereof.

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Presentation OutlinePresentation Outline• DefinitionsDefinitions

•• Biomass Properties Biomass Properties

•• Biomass GasifiersBiomass Gasifiers

•• Combined Heat and PowerCombined Heat and Power

•• Transportation FuelsTransportation Fuels

9/1/2006 4

There are a number of reasons for considering gasification based processes

• Gasification can handle a wide range of biomass feedstocks, ranging from woody residues to agricultural residues to dedicated crops without major changes in the basic process. A system can be designed to handle a variety of feeds

• Gasification is applicable across a wide-range of sizes, e.g., farm, village, small industry or town, to large-scale industrial

• The thermal efficiency of gasification based processes can be high

• CHP – up to 90%

• 1st generation fuels processes – up to 60%

• Fuels and chemicals synthesis processes from syngas are already commercial

• Gasification-based CHP can maximize the renewable character of existing and proposed ethanol projects.

9/1/2006 5

ThermalConversion

Combustion Gasification Pyrolysis

(CO + H2)

No AirPartial airExcess air

ThermalConversion

Combustion GasificationPyrolysis &

Hydrothermal

Heat Fuel Gases (CO + H2

Liquids

No AirPartial airExcess air

The primary conversion routes give different types of products

9/1/2006 6

Gasification Cleanup Synthesis

Conversionor Collection Purification

Separation Purification

Pyrolysis

OtherConversion *

Biomass

* Examples: Hydrothermal Processing, Liquefaction, Wet Gasification

• Hydrogen• Alcohols• FT Gasoline• FT Diesel• Olefins• Oxochemicals• Ammonia• SNG

• Hydrogen• Olefins• Oils• Specialty Chem

• Hydrogen• Methane• Oils• Other

Fungible fuels & chemicals are major products. New classesof products (e.g., oxygenated oils) require market development

9/1/2006 7

Pyrolysis is defined as• Thermal conversion (destruction) of organics in the absence of oxygen • In the biomass community, this commonly refers to lower temperature thermal

processes producing liquids as the primary product• Possibility of chemical and food byproducts

Gasification is defined as• Thermal conversion of organic materials at elevated temperature and

reducing conditions to produce primarily permanent gases, with char, water, and condensibles as minor products

• Primary categories are partial oxidation and indirect heating (steam gasification)

Combustion is defined as• Thermal conversion of organic matter with an oxidant (normally oxygen)

to produce primarily carbon dioxide and water• The oxidant is in stoichiometric excess, i.e., complete oxidation

Combustion, pyrolysis, and gasification are the primary types of thermochemical conversion processes

9/1/2006 8

Primary Processes Secondary Processes Tertiary Processes

VaporPhase

LiquidPhase

SolidPhase

Low P

HighP

Low P

HighP

Biomass Charcoal Coke Soot

PrimaryLiquids

PrimaryVapors

Light HCs,Aromatics,

& Oxygenates

Pyrolysis Severity

Condensed Oils(phenols, aromatics)

CO, H2,CO2, H2O

PNA’s, CO, H2, CO2,

H2O, CH4

Olefins, AromaticsCO, H2, CO2, H2O

CO, CO2,H2O

Gasification involves primary, secondary, and tertiary reactions

9/1/2006 9

To understand thermochemical conversion we need to know the physical and thermal properties that influence thermal behavior

9/1/2006 10

Poplar Corn Stover Chicken Litter Black LiquorProximate (wt% as received)

Ash 1.16 4.75 18.65 52.01Volatile Matter 81.99 75.96 58.21 35.26Fixed Carbon 13.05 13.23 11.53 6.11Moisture 4.80 6.06 11.61 9.61

HHV, Dry (Btu/lb) 8382 7782 6310 4971

Ultimate, wt% as received

Carbon 47.05 43.98 32.00 32.12Hydrogen 5.71 5.39 5.48 2.85Nitrogen 0.22 0.62 6.64 0.24Sulfur 0.05 0.10 0.96 4.79Oxygen (by diff) 41.01 39.10 34.45 0.71Chlorine <0.01 0.25 1.14 0.07Ash 1.16 4.75 19.33 51.91

Elemental Ash Analysis, wt% of fuel as received

Si 0.05 1.20 0.82 <0.01 Fe --- --- 0.25 0.05 Al 0.02 0.05 0.14 <0.01 Na 0.02 0.01 0.77 8.65 K 0.04 1.08 2.72 0.82 Ca 0.39 0.29 2.79 0.05 Mg 0.08 0.18 0.87 <0.01 P 0.08 0.18 1.59 <0.01 As (ppm) 14

Representative Biomass & Black Liquor Compositions

The basic properties for the comparison of thermal behaviorare proximate and ultimate analyses

9/1/2006 11

The heating value is important in estimating process efficiency

Biomass Higher Heating Value

Correlation HHV, MJ/kg

10 15 20 25 30

Expe

rimen

tal H

HV,

MJ/

kg

10

15

20

25

30

Regression, r2=0.834, n = 17999% CIAquatic Herbaceous RDF WoodyLigninAnimal Waste

High Ash

Low Ash

HHV = 0.349C + 1.178H + 0.1005S - 0.1034O - 0.015N - 0.211A

Channiwala, S.A. and P.P. Parikh (2002), Fuel, 81, 1051-1063

MAF Higher Heating Valueas a Function of MAF C, H, O

Predicted HHV (MJ/kg)

16 18 20 22 24 26 28

Expe

rimen

tal H

HV

(MJ/

kg)

16

18

20

22

24

26

28

HHV (MJ/kg) = 0.364C + 0.319H - 0.00381Or2 = 0.764, n = 179

9/1/2006 12

Potassium Content of Biomass

0.0 0.5 1.0 1.5 2.0 2.5 3.0 3.5

Mixed waste paperFir mill waste

RFD - TacomaRed oak sawdust

Sugar Cane BagasseUrban wood waste

Willow - SV1-3 yrFurniture waste

Willow - SV1-1 yrAlder/fir sawdust

Switchgrass, MNHybrid poplar

Switchgrass, D Leaf, MNDemolition woodForest residuals

Poplar - coarseMiscanthus, Silberfeder

Wood - land clearingAlmond wood

Wood - yard wasteDanish wheat straw

Rice husksSwitchgrass, OH

Oregon wheat strawAlfalfa stems

California wheat strawImperial wheat straw

Rice straw

Potassium Content (lb/MBtu)

Bain, R. L.; Amos, W. P.; Downing, M.; Perlack, R. L. (2003). Biopower Technical Assessment: State of the Industry and the Technology. 277 pp.; NREL Report No. TP-510-33123

Potassium content influences slagging, fouling,and pyrolysis oil properties

9/1/2006 13

Nitrogen Content of Biomass

0.0 0.5 1.0 1.5 2.0 2.5 3.0 3.5

Red oak sawdustFir mill waste

Mixed waste paperSugar Cane Bagasse

Urban wood wasteFurniture waste

Miscanthus, SilberfederWillow - SV1-3 yr

Wood - land clearingDanish wheat straw

Alder/fir sawdustOregon wheat straw

California wheat strawDemolition wood

Poplar - coarseImperial wheat straw

Hybrid poplarWillow - SV1-1 yr

Rice husksSwitchgrass, MN

Almond woodSwitchgrass, D Leaf, MN

Switchgrass, OHBana Grass, HI

Forest residualsRFD - Tacoma

Wood - yard wasteRice straw

Alfalfa stems

Nitrogen (lb/MBtu)

Bain, R. L.; Amos, W. P.; Downing, M.; Perlack, R. L. (2003). Biopower Technical Assessment: State of the Industry and the Technology. 277 pp.; NREL Report No. TP-510-33123

Nitrogen is important in determining the needfor NOx emission mitigation strategies

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Gasification has a long history of development and useMurdoch (1792) coal distillation

London gas lights 1802

Blau gas – Fontana 1780

1900s Colonial power

MeOH 1913 BASF

Fischer Tropsch 1920s

Vehicle Gazogens WWII

SASOL 1955 - Present

GTL 1995 – Present

Hydrogen – Future?

Circa 1898

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4%8%

11%

23%

53%

ammonia

refineries (H2)

methanol

electricity

gas-to-liquids

other

A. van der Drift, R. van Ree, H. Boerrigter and K. Hemmes: Bio-syngas: key intermediate for large scale production of green fuels and chemicals. In: The 2nd World Conference on Biomass for Energy, Industry, and Climate Protection, 10-14 May 2004, Rome, Italy, pp. 2155-2157 (2004).

The world syngas market is approximately 6 EJ/yr

9/1/2006 16

Bio

mas

s

Primary Conversion Tar Removal Syngas Conditioning Biofuel Synthesis

Dry-AshGasifier

Direct

Indirect

SlaggingEntrained-Flow

Gasifier

Or

High-TempThermal

Tar Cracking

FastPyrolysis

SlowPyrolysis

Torrefaction

CatalyticReforming Filter

Quench

SulfurRemoval

Shift

TraceRemoval

Ethanol

Mixed Alcohols

F-T Liquids

Methanol

DME

OtherHydrogenAmmonia

SNG

There are a numberof gasification pathways

Source: ECN (2006), ECN-C-06-001

9/1/2006 17

Freeboard

Fluid Bed

PlenumAir/Steam

Biomass

Ash

Cyclone

Fluid-Bed Gasifier

Freeboard

Fluid Bed

PlenumAir/Steam

Biomass

Ash

Cyclone

Fluid-Bed Gasifier

Secondary

Circulating Fluid-Bed Gasifier

Fly Ash

Bottom Ash

Biomass

Air/Steam

GasifierPrimaryCyclone

CycloneSecondary

Circulating Fluid-Bed Gasifier

Fly Ash

Bottom Ash

Biomass

Air/Steam

GasifierPrimaryCyclone

Cyclone

Fly Ash

Bottom Ash

Biomass

Air/Steam

GasifierPrimaryCyclone

Cyclone

Biomass

Pyrolysis

Reduction

Combustion

Gas, Tar, Water

AshAir

C + CO2 = 2COC + H2O = CO + H2

C + O2 = CO24H + O2 = 2H2O

Downdraft Gasifier

Biomass

Pyrolysis

Reduction

Combustion

Gas, Tar, Water

AshAir

C + CO2 = 2COC + H2O = CO + H2

C + O2 = CO24H + O2 = 2H2O

Downdraft Gasifier

Biomass

N2 or Steam

Furnace

Char

Recycle Gas

ProductGas

Flue Gas

Entrained Flow Gasifier

Air

Biomass

N2 or Steam

Furnace

Char

Recycle Gas

ProductGas

Flue Gas

Entrained Flow Gasifier

Air

Pyrolysis

Reduction

Combustion

Gas, Tar, Water

Ash

Biomass

Air

C + CO2 = 2COC + H2O = CO + H2

C + O2 = CO24H + O2 = 2H2O

Updraft Gasifier

Pyrolysis

Reduction

Combustion

Gas, Tar, Water

Ash

Biomass

Air

C + CO2 = 2COC + H2O = CO + H2

C + O2 = CO24H + O2 = 2H2O

Updraft Gasifier

QUENCHWATER

OXYGENFEED SLURRY

NATURALGAS

SYNGAS

SLAG

WATER

Entrained-FlowSlagging Gasifier

There are a number of types of biomass gasifiers –e.g., fixed bed, fluid bed, and entrained flow

9/1/2006 18

Each gasifier has advantages and disadvantages

Gasifier Advantages Disadvantages Updraft Mature for heat

Small scale applications Can handle high moisture No carbon in ash

Feed size limits High tar yields Scale limitations Producer gas Slagging potential

Downdraft Small scale applications Low particulates Low tar

Feed size limits Scale limitations Producer gas Moisture sensitive

Fluid Bed Large scale applications Feed characteristics Direct/indirect heating Can produce syngas

Medium tar yield Higher particle loading

Circulating Fluid Bed Large scale applications Feed characteristics Can produce syngas

Medium tar yield Higher particle loading

Entrained Flow Can be scaled Potential for low tar Potential for low CH4 Can produce syngas

Large amount of carrier gas Higher particle loading Potentially high S/C Particle size limits

9/1/2006 19

Efficient biomass gasifiers exploit the unique characteristics of biomass

Characteristic

Fibrous material

High reactivityHigh volatiles contentHigh char reactivity

Raw syngas compositionTarsSulfurAlkali, ammonia, others

Scale of Operation

Implications

Feeding systems:

Particle size limitations, pressurized operation more difficult

Gasifier design

Allows gasification without pure oxygen

Gas cleanup

More tar, water solubleLow sulfur (except BL)Must be considered

Limits economies of scale

9/1/2006 20

Low(300-600°C)

Medium(700-850°C)

High(900-1200°C)

LowPressure

0.2 MPa

HighPressure

ENSYNDynamotiveBTGFortum

Bio-OilChanging World

TechnologiesChemrec (O2)Future Energy (Siemens)

GTI (O2)Carbona (O2)HTW O2)Foster Wheeler (O2)

FERCO (Indirect)MTCI (Indirect)Pearson (Indirect)TUV (Indirect)

For CHP:TPS (Air)Carbona (Air)Lurgi (Air)Foster Wheeler (Air)EPI (Air)Primenergy (Air)Community PowerFrontline

Chemrec (Air)

Feed: Biomass Feed: Black LiquorFeed: Biomass

MTCI-also BlackLiquor

Gas Product: PNNL Wet Gasification (CH4/H2)

10-25 MPa 1- 3 MPa 2 – 3 MPa

SyngasProductDry Ash Slag

Choren – 2 stage

A large number of companies are involved inbiomass thermal conversion

9/1/2006 21

Gasifier FERCO Carbona Princeton IGTModel

Type Indirect CFB Air FB Indirect FB PFBAgent steam air steam O2/steamBed Material olivine sand none aluminaFeed wood chips wood pellets black liquor wood chips

Gas Composition H2 26.2 21.7 29.4 19.1 CO 38.2 23.8 39.2 11.1 CO2 15.1 9.4 13.1 28.9 N2 2 41.6 0.2 27.8 CH4 14.9 0.08 13.0 11.2 C2+ 4 0.6 4.4 2.0GCV, MJ/Nm3 16.3 5.4 17.2 9.2

Gas compositions vary according to gasifier type

9/1/2006 22

Gasifier Inlet Gas Product Gas Product GasType HHV

MJ/Nm3

Partial Oxidation Air Producer Gas 5-7Partial Oxidation Oxygen Synthesis Gas 10Indirect Steam Synthesis Gas 15

Natural Gas 38Methane 41

Typical gas heating values vary from 15% to 40% of natural gas heating value

9/1/2006 23

Small and medium size combined heat and power is a good opportunity for biomass

9/1/2006 24

DOE and the USDA Forest Service have supported developmentCommunity Power Corporation’s BioMax Modular Biopower System

5, 15, 50 kW systems

9/1/2006 25

CPC’s direct air gasification produces no waste water

70% of Biomass Energy = Chemical Fuel15% of Biomass Energy = Recoverable Heat, Gas Cooling

Pyrolysis Air(Primary)

Dry Biomass Feed

Coarse Filter

Gas Application

Fine Filter< 0.7 µmCooling Air

750°C

80°C

Feedstock DryerOr Heat Application

Char Air

Pyrolysis (900°C)

Tar Cracking(900 to 1000°C)

22% CO16% H210% H2O9% CO23% CH440% N2

9/1/2006 26

DOE, the European Union, the Danish government, Skive Fjernvarme, and Carbona are cooperating in the 5MWe Carbona Project in Skive, Denmark

BIOMASSBIOMASS

ASHASH

AIRAIR

ASHASH

POWERPOWER

HEATHEAT

FUELFUELFEEDINGFEEDING

GASIFIERGASIFIERTAR CRACKERTAR CRACKER

GAS COOLERGAS COOLER GAS COOLERGAS COOLERSTACKSTACK

HEAT RECOVERYHEAT RECOVERY

GAS TANKGAS TANK

GAS ENGINE(S)GAS ENGINE(S)

BIOMASSBIOMASS

ASHASH

AIRAIR

ASHASH

POWERPOWER

HEATHEAT

FUELFUELFEEDINGFEEDING

GASIFIERGASIFIERTAR CRACKERTAR CRACKER

GAS COOLERGAS COOLER GAS COOLERGAS COOLERSTACKSTACK

HEAT RECOVERYHEAT RECOVERY

GAS TANKGAS TANK

GAS ENGINE(S)GAS ENGINE(S)

• 110 tpd wood pellets• 5.4 MW electric power• 11.5 MW thermal• 30, elec LHV eff, 90% overall

9/1/2006 27

http://www.primenergy.com/Projects_detail_LittleFalls.htm 8/28/06

Producers are starting to use biomass gasifiersfor CHP in corn ethanol facilities

•Central Minnesota Ethanol Cooperative (CMEC)•15million gpy ethanol plant in Little Falls, MN•Funding – USDA, XCEL Energy, Private•E&C – Sebesta Blomberg•Gasifier – Primenergy•280 tpd wood•50 k-lb/hr high pressure steam for electricity•35 MMBtu/hr thermal energy

9/1/2006 28

Chippewa Valley Ethanol Company has entered into an agreement with Frontline Bioenergy to support the installation of a prototype gasifier at the CVEC Benson, MN ethanol plant.

• The objective is to replace all of the plant’s natural gas usage

• 45 mil gal/yr plant with $20 million in annual natural gas costs

• $3.4 million in research services• $12.4 million in equipment and materials

Source: frontlinebioenergy.com 8/29/06

9/1/2006 29

Transportation fuels production will probably be at larger scalebecause of process complexity and capital intensive nature. There may be opportunities for smaller modular “skid mount”systems.

Feed PrepBiomass

Dryer

Gasification (BCL, & cyclones)

Scrubber Syngas Compression

Char & Sand

Char combustor & cyclonesAir

SteamFlue gas

Tar reformer

Sand

Ash

Water

Totreatment

LO-CAT

Sulfur

Amine System

CO2

Gas Compression

Mixed Alcoholssynthesis

Gas

purge

Separation Amine System

CO2

Tar reformer catalyst regenerator

Natural gas

Steam cycle

Air

Catalyst

Liquids

Mol sieve Separation EtOH

C3+ alcohols

MeOH

H2O

Separation

C2+ alcohols

to atm

Feed PrepBiomass

Dryer

Gasification (BCL, & cyclones)

Scrubber Syngas Compression

Char & Sand

Char combustor & cyclonesAir

SteamFlue gas

Tar reformer

Sand

Ash

Water

Totreatment

LO-CAT

Sulfur

Amine System

CO2

Gas Compression

Mixed Alcoholssynthesis

Gas

purge

Separation Amine System

CO2

Tar reformer catalyst regenerator

Natural gas

Steam cycle

Air

Catalyst

Liquids

Mol sieve Separation EtOH

C3+ alcohols

MeOH

H2O

Separation

C2+ alcohols

to atm

9/1/2006 30

Hydrocarbon fungibility will be a key to successPrimary Energy

Source Syngas Step Conversion Technology Products

Syngas(CO + H2)

Fischer Tropsch

(FT)Upgrading

Lubes

Naphtha

DieselSyngas to Liquids (GTL) Process

Mixed Alcohols (e.g. ethanol, propanol)

Syngas to Chemicals Technologies

Methanol

Acetic Acid

Others (e.g. Triptane, DME, etc)

Coal

Natural Gas

Biomass

Hydrogen

Extra Heavy

Oil

Source: BP

9/1/2006 31

Integrated biorefineries involve both biochemical and thermochemical processes

9/1/2006 32

A 30x30 advanced integrated biorefinery scenario, i.e., the E85 Refinery, includes both thermochemical and biochemical processing

Ethanol yield = 94 gal/dry ton stoverGasoline yield = 90 gal/dry ton of lignin (13 gal/ton of stover)

(Plant total Ethanol equivalent yield = 118 gal/dry ton stover)

Ethanol via bioconversionCorn Stover

10,000 dMT/day

Ethanol1,035,000 gpd36.2 MM gal/yr

Lignin-rich Residue 1,500 dMT/day

Steam &Power

Selective thermal processing

Gasoline148,011 gpd

(Diesel is recycled to produce a lignin slurry feed)

Lignin-rich Residue 1,432 dMT/day

LigninCHP Plant

Diesel5,911 gpd

Minimum gasoline selling price = $0.51/gal gasoline(Minimum Ethanol equivalent selling price = $0.35/galEtOH)

Plant Minimum Ethanol equivalent selling price = $0.57/gal EtOH

9/1/2006 33

Methanol from BiomassComparison of Capital Investment

(2002$)

Cap

ital I

nves

tmen

t ($/

annu

al g

al M

etha

nol e

q)

1.00

1.50

2.00

2.50

3.00

3.50

4.00

4.50

5.00

Atmospheric O2 slaggingentrained flow

Pressurized O2fluid bed

Pressurized O2fluid bed

Pressurized O2fluid bed

Pressurized O2 slaggingentrained flow

Indirect steam

Indirect steamIndirect steam

Indirect steam withcatalytic reforming

Indirect Steam withhot particulate removal

Wyman, et al., 19932000 tpd biomass

Hamelinck & Faaij, 20012000 tpd biomass

Katofsky, 19931815 tpd biomass

rlb, 08/25/06

Although ethanol and Fischer-Tropsch liquids are presently preferredproducts, previous work on methanol can help guide analysis

9/1/2006 34

Analysis of ethanol from TC mixed alcohols shows the potential to reach the DOE goal of $1.07/gal in 2012

$0.00

$0.50

$1.00

$1.50

$2.00

$2.50

2000 2005 2010 2015 2020

Min

imum

Eth

anol

Sel

ling

Pric

e ($

per

gal

lon) Conversion

FeedstockPrevious DOE Cost TargetsPresident's Initiative

State of Technology Estimates

Integrated with Biochemical Processing

104 gal/ton total yield

Biorefinery Residues67 gal/ton

Costs in 2002 Dollars

ForestResources56 gal/ton

9/1/2006 35

Questions and Answers

9/1/2006 36

What is the scale of proposed processes?

The scale can range from 15 kg/hr for home-based systemsto 400 tons/hr for large nth plant central facilities.

9/1/2006 37

What feedstocks care appropriate for gasification?

Almost any biomass feed is suitable. Certain high moisture feeds like wet manure may be uneconomic because of high drying costs. Feeds high in potassium, e.g., alfalfa, may require special processing.

9/1/2006 38

What feed preparation, storage, and handling is required?

Feed preparation is specific to the gasifier being used.

• Certain gasifiers require defined particle sizes, e.g., downdraft – no fines, or entrained flow - very small particles. Almost all gasifiers require particle size less than 1.5 inches.

• Others require low moisture content, e.g. downdraft

Typically screening of oversize materialand metal removal is required

Storage requirements are standard. On site typically 3 – 7 days.

Handling requirements are a function of the form of biomass at the plant gate.

9/1/2006 39

What are the estimated efficiency of gasification processes?

Gasification efficiency is a function of the feed, gasification process and final product. Typical values from operating experience and technoeconomic analyses are.• Combined heat and power, 90%• Electricity only, 25 – 35%•Methanol, 60%•DME, 54%•FTL, 45%•Mixed alcohols, 40-45%

9/1/2006 40

What co-products could be marketed, and what further processing would they require?

This is process specific. An example would be a mixed alcohols process where higher alcohols could be produced along with ethanol. Generally, separation and purification to meet commercial specifications is required. Specifications are generally defined by ASTM standards.

9/1/2006 41

How would product quality be assured?

through standard business practices defined by contracts and standards

9/1/2006 42

What equipment maintenance would be required, and how would maintenance be handled?

This is project specific.

It will be a function of project size.

9/1/2006 43

What are the emissions and waste disposal issues or uncertainties?

All processes have to be permitted and limits are set by the permitting agencies. Emissions estimates based on existing processes can beused, e.g., EPA AP-42 for CHP, or can be estimated by E&C contractors.

Probably the biggest unkown is ash disposal.

9/1/2006 44Illustration by Oak Ridge National Lab

9/1/2006 45

There are technical barriers needing addressing in the major processing steps in thermochemical conversion

Feed Processing

and Handling

Gasification

Pyrolysis

Gas Cleanup

High T Separation

Gas Conditioning

Collection/Fractionation

Fuel Synthesis

Upgrading

Heat&

Power

• Size Reduction• Storage and Handling• De-watering• Drying

• Partial Oxidation• Air blown• Oxygen blown• Indirect

• Flash pyrolysis• Steam pyrolysis• Vacuum pyrolysis

• Particulate removal• Tar reforming• Benzene removal• S, N, Cl mitigation

• High T Filtration• Alkali removal

• Methane reforming• CO2 removal• H2/CO adjustment• Sulfur polishing

• Aerosol collection• Microfiltration• Chemical Stabilization• Hydrotreating• Dehydration

• C1 chemistry– FT liquids– MTG– Mixed OH

• Upgrading• Production Separation

9/1/2006 46

Barriers and R&D needs were identified by a panel of expert stakeholders at the DOE 30 x 30 Workshop in August

• Technology issues with scale and syngas quality, and process integration• Feeder systems• Gas cleanup: tars, sulfur, particulates, etc.• Matching scale to economy• Lack of demonstration plants

• Other• Business links: fuel resources > conversion > product distribution• Competition between biomass, coal, natural gas, and tar sands for talent, construction materials, capital• Competing markets for resources• Permitting issues

9/1/2006 47

The 30 x 30 panel also developed a set of R&D needs

• Feeders (solid biomass)• High temperature materials, esp. for black liquor gasification• Syngas conversion to match scale – better processes/catalysts• Gas cleanup• Gasifier type• Blended fuels• Technology demonstrations