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The Future of R&D Requirements for qOxyfuel Combustion
-Activities in Japan-
Ken OKAZAKIDean School of Engineering
-Activities in Japan-
Dean, School of EngineeringProfessor, Dept. of Mechanical and Control Engineering
Tokyo Institute of Technology (Tokyo Tech), Japan
Takashi KIGATakashi KIGAPower Plant Division
IHI Corporation, Japan
C i R t Y A t li
Tokyo Institute of TechnologySchool of Engineering
Capricorn Resort Yeppoon, Australia 13th September, 2011
“Oxy-fuel combustion for power At the beginning
y pgeneration and carbon dioxide (CO2) capture”
Editted by Ligang Zheng
Part IIntroduction to oxy fuel combustion
Contents
Introduction to oxy-fuel combustionPart II
Oxy-fuel combustion fundamentalsPart IIIPart III
Advanced oxy-fuel combustion concepts and developments
Tokyo Institute of TechnologySchool of Engineering
Oxy-Coal CombustionAt the beginning
Presentations2004 No presentation2005 One presentation2005 One presentation2006 One session2007 Full sessions (full of audience)… …2011 Full sessions (full of audience)
Panel: Oxy-Fuel TechnologyOxy-Fuel Technology I : Overview & DemonstrationsO F l T h l II E i iOxy-Fuel Technology II : EmissionsOxy-Fuel Technology III: Experimental StudiesOxy-Fuel Technology IV: Understanding Oxy-Combustion Impacts
Tokyo Institute of TechnologySchool of Engineering
Oxy-Fuel Technology V : Burner Developments
US: FutureGen ProjectEU: Proposal under the NER300
2 Oxyfuel CCS projects were applied
At the beginning
"This investment in the world's
Announce of US DOE
US: FutureGen Project 2 Oxyfuel CCS projects were applied for a share of funding from NER300
This investment in the world s first, commercial-scale, oxy-combustion power plant will help to open up the over $300 billion
f J h ldmarket for coal unit repowering and position the country as a leader in an important part of the global clean energy economy."
Janshwalde Project(Germany)
global clean energy economy.
Dr. Steven ChuU.S. Secretary of EnergyA t 5 2010
Drax Project August 5, 2010
j(Yorkshire)(England)
Tokyo Institute of TechnologySchool of Engineering< Source by Homepage of US DOE > < Source by Homepage of NER300 >
Contents
Oxyfuel Development History in JapanOxyfuel Development History in JapanBasic Study ItemsStudy items for DemonstrationStudy items for DemonstrationFuture StudyConclusionConclusion
Tokyo Institute of TechnologySchool of Engineering
200 FutureGen/B&W
DemoDemo.
Bench/Pilot
Terry Wall, IEA 1st Oxyfuel Combustion Conference, 2009
Tokyo Institute of TechnologySchool of Engineering6
O2/CO2 (Oxy-firing) Coal CombustionConventional pulverized coal combustionConventional pulverized coal combustion
CO2 concentration in flue gas is about 13 %
Great energy consumption to separate CO22
O2/CO2 pulverized coal combustion
CO2 concentration in flue gas is enriched up
to 95 %Easy and efficient CO2 recoveryto 95 %
O2
Coal
O d tiAir Furnace
Practically realized by IshikawajimaharimaCo., Ltd. ASU
Small amount of exhausted gas (extremely low amount of
2O2 production Furnace
Oxy-firing of coal
Tokyo Institute of TechnologySchool of Engineering
( yNOx, SOx)Recycled gas<Okazaki, Ando, ENERGY, 1997>
Study Items for Commercialization
O d ti & l Oxyfuel Plant (Integrated operation)Oxygen production & supply Method & System oxygen purity
Oxyfuel Plant (Integrated operation)Performance (Boiler Efficiency, CO2 capture rate)Control (Oxyfuel, MFT)Operation(Mode change, Load range, Start-up, Shut-down)Durability and Safety
CoalBoiler
AH FFFGLPH
Durability and Safety
CO2 Capture ProcessSystem Optimization
GRF
AH
Stack
FGLPH
Mill
O2Air
N2
System OptimizationImpurities RemovalOutlet CO2 Properties
CO2 liquefaction
Non-condensable gas(CO2, H2O, SO2…)
<Oxyfuel boiler>
ASU
<Oxygen production & supply>
O f l B il (F )
CO2 tankFlue gas treatment & compressor Cold Box
Oxyfuel Boiler (Furnace)Combustion characteristicsFlame stabilityRadiation heat transfer Oxyfuel Boiler (Flue Gas)
C i E i t
Tokyo Institute of TechnologySchool of Engineering
< CO2 capture process > Corrosion Environment Trace Element
Oxyfuel system development history in JapanNow
201520102005200019951990Now
2020
Demonstration ReadyBasic Study(NEDO)(NEDO)
Feasibility Study(NEDO)
The first national Oxyfuel R&D project in Japan
Japan and Australia Joint Demonstration Project
( )
Callide Project(METI/NEDO)
Application Study
Demonstration
Future Study
Oxyfuel basic study was performed from 1990 Demonstration Ready by the end of 1990’s
Tokyo Institute of TechnologySchool of Engineering
Demonstration Ready by the end of 1990 s Demonstration Project was conducted from 2004, and operation will stat soon
Oxyfuel system development history in Japanal
e
Commercial
Sca
Pilot Plant (Horizontal)
Pilot Plant (Vertical)
Drop Tube Furnace Ignition apparatus Ignition apparatus
under Micro-gravity
Large Scale DemonstrationCallide-A
Tokyo Institute of TechnologySchool of Engineering
Time1990 1993 2011 2015~1998
Pilot plant and demo plant
Pilot Plant(Horizontal)
Pilot Plant(vertical)
Demo Plant(Callide)(Horizontal) (vertical) (Callide)
Capacity Max. 150kg/h(Coal)(1.2MW thermal)
30MWe(100MWth)
Furnace I D 1 3m x L 7 5m Steam GeneratorFurnace I.D. 1.3m x L 7.5m Steam GeneratorYear 1993 1998 2011
Photo
Tokyo Institute of TechnologySchool of Engineering
Basic Study Items
Coal jet ignition Chemistry Burner aerodynamics and heat transfery
Char burnout SOx
Ash partitioning Ash partitioning Deposition Trace elements
Combustion by-products Combustion by products NOx, SOx
Heat transfer Radiant zone Radiant zone Convective zone
Tokyo Institute of TechnologySchool of Engineering
NOx reduction in Oxyfuel
Pulverized Coal + Gas
Alumina tube
Heater To Exhanst
To Analysis
Combustion Efficiency and NOx Conversion Ratio
NOx Reduction Ratio(doped NOx in combustion gas)
Drop Tube Furnace
< Kiga, Thermal Energy Symposium,1992 >g , gy y p ,
Combustion Efficiency was not changed by substitution of CO2 for N2 NOx comversion ratio decrease with increase the CO2 substitution NOx is possible to be reduced by gas recycle into flame
Tokyo Institute of TechnologySchool of Engineering
NOx is possible to be reduced by gas recycle into flame
Mass balance of N-atoms
System CR*Exhausted-NExhausted N
Fuel-N=
local CR and local RR wereexperimentally identified.
Tokyo Institute of TechnologySchool of Engineering
<Okazaki, Ando, ENERGY, 1997>
d ffi i COEasy and efficient CO2d ffi i COEasy and efficient CO2
Further NOx Reduction by Heat Recirculation
CaCO3
Easy and efficient CO2
separation · recovery
High
Easy and efficient CO2separation · recovery
CaCO3
Easy and efficient CO2
separation · recovery
High
Easy and efficient CO2separation · recovery
<Liu & Okazaki FUEL 2003>3
Small amount of
CoalO2
High concen-tration CO2
Furnace
3
Small amount of
CoalO2
High concen-tration CO2
Furnace
<Liu & Okazaki, FUEL, 2003>
exhausted flue gas(Extremely low NOx,SOx)
CO2
Recycled heat SOx emissions)
exhausted flue gas(Extremely low NOx,SOx)
CO2
Recycled heat SOx emissions)SOx)
Recycled gas (Mainly CO2 including NOx, SOx)
Intensify coal combustionDecrease NO further
Additional merits
SOx emissions)SOx)
Recycled gas (Mainly CO2 including NOx, SOx)
Intensify coal combustionDecrease NO further
Additional meritsIntensify coal combustionDecrease NO further
Additional merits
SOx emissions)
Decrease NO further through combustion with low O2 concentrationImprove fuel flexibilityB d l d h
Schematic of O2/CO2 Coal Combustion ith b th d h t i l ti
Decrease NO further through combustion with low O2 concentrationImprove fuel flexibilityB d l d h
Decrease NO further through combustion with low O2 concentrationImprove fuel flexibilityB d l d h
Schematic of O2/CO2 Coal Combustion ith b th d h t i l ti
Schematic of O2/CO2 Coal Combustion ith b th d h t i l ti
Tokyo Institute of TechnologySchool of Engineering
Broaden load change range of a boiler
with both mass and heat recirculation Broaden load change range of a boilerBroaden load change range of a boiler
with both mass and heat recirculationwith both mass and heat recirculation
Drastic Reduction of CR* (Fuel-N to NOx) by Oxy-firing
Base caseC ti l
Oxy-fuelO2 : 30% O f l
ConventionalO2 : 21%H.R.: 0%
O2 : 30%H.R.: 0%
Oxy-fuelO2 : 21%H.R.: 0%
Oxy-fuelO2 : 15%H.R.: 40%
<Liu & Okazaki, FUEL, 2003>
Tokyo Institute of TechnologySchool of Engineering
The first oxyfuel combustion trial in 1993Initial Combustion TestInitial Combustion Test
Difficult of holdingp. [d
egC
]
Air (Wind-box O2: 21%)
Difficult of holding the stable flame in case of wind-box O2 of 21% in Distance from burner exit [m]
Flam
e Te
m
oxyfuelm
e Te
mp.
[deg
C]
Oxyfuel (Wind-box O2: 21%)Need to increase the inlet-O2 in order to keep the stable flame and
Distance from burner exit [m]
Flam
egC
]
stable flame and radiation heat transfer
Flam
e Te
mp.
[de
Tokyo Institute of TechnologySchool of Engineering
Oxyfuel (Wind-box O2: 30%)
17
Distance from burner exit [m]
< NEDO Report, 1993 >
Flame Propagation Velocity in High CO2 Concentration30mm
Coal A(N2/O2)
Coal B(N2/O2)
Coal C(N2/O2)
Coal A(CO2/O2)
Coal A N2/O
2
1.5Ignition
5ms Coal A(CO2/O2)
Coal C(CO2/O2)1.0
5ms
10ms
Bright Low light
Coal C CO2/O
2
Coal C N2/O
2
Coal A CO2/O
2
0
0.5
15ms
20ms
light
Flame propagation behavior
0 1 2 3 4
Coal concentration [kg/m3]
0
Result of gravity-free experiment
Coal A, N2/O2 Coal C, N2/O2 Coal C, CO2/O2
In CO2/O2, flame brightness reduces and flame becomes unstable.
< Suda, et al, IHI Engineering Review, 1999 >By using a microgravity condition, effect of natural convection and buoyancy can be neglected, and experiment data can be directly compared with numerical simulation.
Tokyo Institute of TechnologySchool of EngineeringCopyright © 2008 IHI Corporation All Rights Reserved.
2 2, g Flame propagation velocity in CO2/O2 largely decrease to 1/3–1/5 of that in N2/O2
One-Dimensional Flame Propagation Model
3
3.5
N2/O2CO2/O2
/ k Δl
x
Ignition source
Tw Radiation Tp(n)
Tg(n) Volatile releaseand combustion
1.5
2
2.5CO2/O2,k=0
In N2/O2
In CO2/O2
Absorption by gas or particle
Scattering by particle
Heat conduction betweengas and particle
x=L=N×Δln=N
Flame position Tp(n)>Tig
Element n=1
0
0.5
1
0 0 5 1 1 5 2 2 5 3 3 5One-Dimensional Model
0 0.5 1 1.5 2 2.5 3 3.5
Coal concentration [kg/m3]
Calculated Results of Flame Propagation Velocity
Large decrease of flame propagation velocity is mainly due to large heat capacity and small thermal diffusivity in CO2/O2
< Suda & Okazaki, FUEL, 2007 >
Tokyo Institute of TechnologySchool of Engineering
and small thermal diffusivity in CO2/O2
NOx Reduction in Pilot Plant Test
Tokyo Institute of TechnologySchool of Engineering
< Takano et al, IHI Engineering Review, 1995 > The effect of oxygen direct injection tothe burner on unburned carbon and NOx
Study items for Demonstration (Callide-A)
Heat AbsorptionCombustibilityCarbon-in-ash
EmissionNOxNOx
Corrosion EnvironmentSOxHgDynamic Characteristics
AuxiliaryAuxiliaryMixing O2 with Recycle flue gas Flame Detector
Tokyo Institute of TechnologySchool of Engineering
Ignition of Fly ash
70 Air case Need to be the same furnace heat absorption in
Simulation of heat absorption
Air Oxy1 Oxy2 Oxy3Total gas flow 142t/h 117t/h 140t/h 170t/h
50
60
70
bsor
ptio
n (M
W)
Air caseOxy case
WB O2: 40wet%
WB O2: 50wet%
pcase of retrofit from air combustion boiler
Total gas flow 142t/h 117t/h 140t/h 170t/h
Total O2 conc. 21% 30.2% 26.5% 21.7%
FEGT Base Lower Nearly equal Higher
Heat absorption Base Lower Nearly equal Higher30
40
20 25 30 35Furn
ace
heat
ab
O2 content of total gas (wetvol%)
WB O2: 30wet%
Air Oxy 1 Oxy 2 Oxy 3Left Front Right Rear Left Front Right Rear Left Front Right Rear Left Front Right Rear
Si l i l h b 2 % f l O i< NEDO Report, 2005 >
Tokyo Institute of TechnologySchool of Engineering
Simulation results suggests that about 27% of total O2 concentration seems to be the same heat absorption in furnace as air combustion
Heat flux and Flame temperature (Pilot plant)
Flame temperatureHeat flux
1800Coal B/Oxy
100 OxyAi
1400
1500
1600
1700
(deg
ree
C.)
Coal B/OxyCoal B/Air
50Flux
Air
1100
1200
1300
Flam
e te
mp.
(50
Hea
t
900
1000
0 1 2 3 4 5 6
Distance from burner throat (m)
T t l O C 27%( t)
00:00 0:10 0:20 0:30 0:40 0:50 1:00
Time
Same level with heat flux at air in case of 27% total O2 Concentration
Total O2 Conc. : 27%(wet)< CCSD Report, 2006 >
Tokyo Institute of TechnologySchool of Engineering
Flame temperature was 50 degree C lower than that of air
Combustion Characteristics (Pilot plant)
10
e(%
) Coal ACoal B
400
500
MJ)
Coal ACoal B
5
sh O
xy m
ode
Coal C
300
400
mod
e (m
g/M
Coal C
Car
bon-
in-a
s
100
200
NO
x, O
xy
00 5 10
CCarbon-in-ash Air mode(%)
00 100 200 300 400 500
NOx, Air mode(mg/MJ)
NO C b i hNOx Carbon-in-ash
NOx emission is reduced in compared with air combustion
*Negative Pressure in Furnace < CCSD Report, 2006 >
Tokyo Institute of TechnologySchool of Engineering
p Carbon-in-ash is also reduced in oxyfuel
Combustion Characteristics (Pilot plant)
20
pm)
Coal ACoal B
2000
m)
Coal ACoal B
10
15
xy m
ode
(pp Coal C
1000
1500
y m
ode
(ppm Coal C
5SO3,
Ox
500
SO2,
Oxy
00 5 10 15 20
SO3 , Air mode(ppm)
00 500 1000 1500 2000
SO2 , Air mode(ppm)
SO SOSO2 SO3
SOx concentration is higher than in air combustion due to recycle
*Negative Pressure in Furnace< CCSD Report, 2006 >
Tokyo Institute of TechnologySchool of Engineering
g y
1000 Coal A-Air
SO3 behavior (Pilot plant)
100
1000
ativ
e nu
mbe
r)
Coal A-AirCoal A-OxyCoal B-AirCoal B-Oxy
: Value is low er limit, in caseof less than detection level
SO3 concentration is rapidly decreased at outlet of air heaterSO3 emission is not detected at the
1
10
SO
3 (-
, rel
a 3stack inlet
air heaterinlet
air heateroutlet
bag filterinlet
bag filteroutlet
SO3 is captured in ash deposit on the heat transfer surface of air heater and the filter of the bag filter
Electrical heater M i P i
This behavior is the same as flue gas in condition of air combustionC i i t ft b
PAF
Stack
IDF
Furnace
Pulverized coal
heater
Bag filter
Gas cooler
Gas cooler
Air heater
Measuring Point
Corrosive environment after bag filter outlet is the same as air combustion
Ai
Pre-mixingBurner Mixing
Tokyo Institute of TechnologySchool of Engineering
AirFDF/GRFElectrical
heaterO2
< Yamada et al, GHGT-10, 2010 >
‐Oxyfuel Hg‐Behavior of Trace Elements (Mercury)
1 1
0.5
Hg
(-)
Hg2+ 0.5
Hg
(-)
Hg2+
0AH inlet AH outlet BF inlet BF outlet
Hg0Dust
0AH inlet AH outlet BF inlet BF outlet
Hg0Dust
AH inlet(450degC)
AH outlet(200degC)
BF inlet(170degC)
BF outlet(120degC)
Gas sampling point (Gas Temp.)
AH inlet(450degC)
AH outlet(200degC)
BF inlet(170degC)
BF outlet(120degC)
Gas sampling point (Gas Temp.)
Gas(Air) Gas(Oxy)
Hg behavior in Oxyfuel was almost the same as Air combustion
Tokyo Institute of TechnologySchool of Engineering
< Gotou et al., ICOPE-11 , 2011>
Ai b ti O f l b ti
Performance of Flame DetectorAir combustion
(PFT : 1400degree C)Oxyfuel combustion
(PFT : 1330degree C)
4
6
ut (V
)
Gain adjustment*PFT:Peak Flame Temperature
-2
0
2
etec
tor s
igna
l out
p
Ai b iO f l b i O f l b i Ai b i
Flame signal On
-6
-4
2
13:00 14:00 15:00 16:00 17:00
Flam
e de Air combustionOxyfuel combustion Oxyfuel combustion Air combustion
Mode change Mode changeMode change
*Self check of detector every 2minutes
Detector signal was generally stable under both air and oxyfuel combustion
Detection signal of the flame at both air and oxyfuel combustion
< Yamada et al , ICOPE-09, 2009 >
Tokyo Institute of TechnologySchool of Engineering
Detector signal was generally stable under both air and oxyfuel combustion. Impact of combustion mode change was very small
O & t th d t ll
O2 mixing with Recycled flue gas
Operation load 100% 100% 80%
O2 conc. & temp. on the duct wall O2 distribution at the inlet of burner wind-box (Optimization of O2 nozzle)
O2BurnerWind-Box Air Heater
Burner load
Nozzle type Type1(Initial)
Type2(Optimum)
Type2(Optimum)
O2 conc. on th d t ll
Burner
the duct wall[%](Max.)
(98%) (34%) (34%)
O2 Injection Nozzle
Wind-BoxInlet
Duct
RFG
Plate
*
O2 conc. at the wind-box inlet [%](Max.-Min.)
(3 3%) (1 3%) (0 7%)
*
Tokyo Institute of TechnologySchool of Engineering*Type of injection nozzle is optimized.
(3.3%) (1.3%) (0.7%)
Future Study on oxyfuel process
ASU (Air Separation Unit)
BTG (Boiler, Turbine, Generator)
CPU (CO2 Compression and Purification Unit)( 2 p )
Upgrading basic model for simulation
SSystem integration
Tokyo Institute of TechnologySchool of Engineering
Improvenent of Net efficiency
Improvement with Higher plant efficiency
Improvement with Scale up and application of membrane separation
Air Separation CO2 Capture assumption
200
250
300
350
oal
onsu
mpt
ion
(t/h)
p 2 p assumptionCapital Power Capital Power
Case1 -30% -30% - - Scale up (7500 ton/d)
Case2 -30% -30% -20% -20% Case 1 + Scale up of CO2 Capture
C 3 40% 60% Application of
3,500CO2 capture (Power)Air separation (Power)Operation & MaintenanceO
2) 30405060
Effi
cien
cy (%
)
Air combustion
200
Co
CoCase3 -40% -60% - - pp
Membrane separation
Case4 -40% -60% -20% -20% Case 3 + Scale up of CO2 Capture
1 500
2,000
2,500
3,000Operation & MaintenanceRetrofit of Boiler (Capital)CO2 capture (Capital)Air separation (Capital)
cost
(JPY
/ton-
CO
900
1000
1100
put (
MW
)
Air combustion
2030
Net
E Oxyfuel
0
500
1,000
1,500
CO
2ca
ptur
e c
700
800
900
Sub-critical(35%)
Supercritical(40%)
A-USC(45%)
Future(50%)
Nel
Out
pOxyfuel
Tokyo Institute of TechnologySchool of Engineering
Case1 Case2 Case3 Case4Base
Feasiblity Study
1000MW t fit t d i JPlant Specification
1000MWe retrofit study in Japan
Study Result
ASU 2 x 500,000 m3N/hBTG 600/620 degC USCCPU 770 t/h
p
Items Cost [billion JPY]
AuxiliaryPower [MW]
Additional Area [m2]
Boiler retrofit 110 30 -
Study Result CPU 770 t/h
BTG (Blue)ASU 295 115 21,000CO2 capture 205 140 17,000
Efficiency Base Oxyfuel [air case] retrofit case
Gross efficiency [%] 44.2 46.0Net efficiency [%] 42.0 33.4
CO2 capture unit
ASU (Pink) Improvement the power consumption for
ASU & CO2 capture unit Compactification or downsizing of ASU &
Tokyo Institute of TechnologySchool of Engineering
(Green)CO2 capture unit< NEDO Report, 2011 >
Dynamic plant simulation
Stack
Pre-cooler &pre-treatmentequipments
O2
Oxygen Pre-heater
Air separation unit
Air
Primarywith P.C.
PGF Inter-cooler
AirGRF/FDFGAH/GGH
EP CO2Compressors
Mill
Feed water heater
Post-treatmentequipments
Boiler
Plant conditionA : Start up(Light off)B : Turbine rollC : Synchronization 300MW
600MW1,000MWRequired time for
ASU hot start-up is approx. 17 hours.
CO2
yD : Turbine master autoE : Combustion changeF : Fuel changeG : Furnace draft control
Combustion mode
300MWCO2capture
Air
A B C E F GD
Oxyfuel
Main fuel
Furnace draft control
Flue gas O2 control
O
Coal
Non-control(Forced draft)
Compressors(Balanced draft)
Air flow(GRF outlet) O2 flow
Recirculation gas flow
Light oil
Tokyo Institute of TechnologySchool of Engineering
Burner WB O2 control Non-control(Air)Recirculation gas flow
(GRF outlet)
Future Study on ASU (Air Separation Unit)
Scale-upSystem optimizationSystem optimizationReducing power consumption Innovative air separation method Innovative air separation method Membrane PSA etc PSA etc.
Tokyo Institute of TechnologySchool of Engineering
Future Study on BTG (Boiler, Turbine, Generator)
Higher plant efficiency Higher Steam Condition (A-USC)g ( ) High temperature material corrosion
Countermeasure against air ingressg gDirect oxy-fuel combustion with minimum or no flue
gas recycleHigh pressure oxyfuel combustion systemChemical-looping combustion for power generation
Tokyo Institute of TechnologySchool of Engineering
Needed Sub-Models for Oxy-PC Furnace
Heat transfer sub-model Radiant zone Convective zone
Ccal jet ignition sub-model Chemistry Burner aerodynamics and heat transfery
Char burnout sub-model SOx
Ash partitioning sub-model Ash partitioning sub model Deposition Trace elements
Combustion by-products Combustion by products NOx, SOx, Hg
Integrated furnace model
Tokyo Institute of TechnologySchool of Engineering
< J.O.L. Wendt, 2007 AIChE Meeting >
Future Study on CPU (CO2 Compression and Purification Unit)
Scale-upProcess optimizationProcess optimizationReducing power consumptionOptimized Pollutant Removal processOptimized Pollutant Removal process NOx SOx Hg, etc.
Tokyo Institute of TechnologySchool of Engineering
Conclusion
The oxyfuel R&D and feasibility study were performed from the beginning of 1990’s for national program infrom the beginning of 1990 s for national program in Japan, and fundamental data was obtained.
Oxyfuel demonstration project is in progress andti ill t toperation will start soon.
Future activities are in study, and we progress toward commercialization and future oxyfuel combustion systemcommercialization and future oxyfuel combustion system
Tokyo Institute of TechnologySchool of Engineering
Thank you for your attention !e-mail: [email protected]
[Acknowledgements]These studies for the demonstration project were greatly supported by METI NEDOThese studies for the demonstration project were greatly supported by METI, NEDO, JCOAL, J-Power and IHI.
Tokyo Institute of TechnologySchool of Engineering
Tokyo Institute of TechnologySchool of Engineering