Oxy-Coal Combustion - Eventos del Instituto de Ingeniería, UNAM

Development in
Oxyfuel Combustion Technologies for
Coal Fired Power Plants with CCS
(Part 1: Boiler and Burner Development)
Stanley Santos
IEA Greenhouse Gas R&D Programme
Cheltenham, UK
Instituto de Inginieria UNAM
28 th March ac 2012

CO2 Capture Options
EPRI 2007
2

Oxy-Coal Combustion Power Plant
Air
Oxygen
Air
separation
Recycled flue gas
Vent
Fuel Boiler Cooling Purification/
(+FGD) compression
CO 2
Steam
Steam
turbine
Power
3
3

Oxy-Combustion Technology
• Use of oxygen instead of air in a boiler – “Oxy-
Combustion” is a feasible option for power plant
with CO2 capture.
• With significant R&D investment in the past decade, this
technology has achieve a maturity similar to the other
leading options for power generation with CCS
• Outline for Presentation
• Boiler and Burner Development
• Air Separation Unit
• Flue Gas Processing Unit
• CO2 Processing Unit
4
4

Oxyfuel Combustion
Overall Schematic Diagram
5

Where Can You Extract the Recycled Flue Gas (RFG)
(For Practical application using low S coal)
6
6

Oxyfuel Combustion Technology
BOILER AND BURNER
DEVELOPMENT
7

Development of Oxy-Fuel Combustion Application in Industry
Adapted from slide of Sho Kobayashi, Praxair
Pictures from IFRF, Air Liqiude, Asahi Glass, Linde Gas
8
8

Historical Perspective – The Early Days
• 1982: Initial suggestion by Abraham et. al.
(OGJ) of using Oxy-Coal Combustion to
produce CO2 for EOR
• 1 st public document looking at capturing CO2 from
flue gas using oxy-combustion.
• However ... as early as 1970’s work has
started din the development of oxy-coal
combustion with recycled flue gas
• 1974: Japan initial conception of using oxy-coal combustion for power
generation. (To reduce pollution)
• 1978: Economic feasibility of oxy-coal combustion was investigated for
EOR application (H. Farzan, Babcock & Wilcox / A. Wolsky, ANL)
9
9

Technology Development
Japan’s initial conception of oxyfuel combustion application
for power generation (1974)
Oxygen
3rd Workshop, IEAGHG International Oxy-Combustion
Network, Yokohama, Japan
10

ANL - EERC Study
World’s 1st Oxy-Coal Combustion Industrial Pilot Scale Study
Tower Furnace (~ 3MWth)
11

Convective Section of the boiler
• heat transfer profile
• ash deposition and fouling issue
Burner design issue
• Ignition
• flame stability
• devolatilisation & char burnout
Radiant Section of the Boiler
• heat transfer profile
• slagging issue
• firesideid corrosion issue
Prior to any retrofit of carbon capture
technology, it is essential to repower
the plant in order to achieve the
highest possible efficiency
12
12

Composition of Comburent
(Oxidant)
Gas Composition
Air Fired Case
Oxy‐Coal Combustion
%v (dry) Pi Primary RFG 2ndary RFG
Nitrogen (N2) 78.1 18 ‐ 12 14 ‐ 10
Oxygen (O2) 20.9 2 ‐ 21 25 ‐ 40
Argon (ar) 0.9 3 ‐ 3.5 3 ‐ 3.5
Carbon Dioxide CO2) 0.04 78 ‐ 60 55 ‐ 40
Water (H2O) %v (wet) < 2 (depend on %RH) 8 ‐ 4 15 ‐ 5
** Calculation based on ~3% air ingress, 95% O2 purity and C 6.87 H 5.56 O 0.56 N 0.13 S 0.03
13
13

Composition of Flue Gas
from Boiler
Gas Composition
%v (dry)
Air Fired Case
Oxy‐Coal Combustion Case
Nitrogen (N2) 80 ‐ 78 14 ‐ 18
Oxygen (O2) 3 ‐ 4 (~3.5) 2 ‐ 5 (~3.5)
Argon (ar) 0.9 ‐ 0.95 3 ‐ 3.5
Carbon Dioxide CO2) 14 ‐ 16 78 ‐ 74
Water (H2O) %v (wet) 6 ‐ 8 20 ‐12
** Calculation based on ~3% air ingress, 95% O2 purity and C 6.87 H 5.56 O 0.56 N 0.13 S 0.03
14 14

Recyled Flue Gas Ratio
Impact to the Flame
Properties
R =
m RFG
m PFG
+ m RFG
15

Optimum Recycle Ratio
(Optimum recycle ratio is defined by the amount of Recycled Flue
Gas to match the heat transfer profile of conventional air fired
operation)
Some of the reported results for the optimum flue gas recycle ratio
Burner Rating
Type of Flue Gas
Molar Ratio 1
(CO2 + H2O)/O2
%O2 in
Comburent 2
Recycle Ratio
MRFG/(MRFG + MPFG)
ANL – EERC
3 MWth
partially dried RFG
(~18%v moisture)
266 2.66 26% (wet) -
wet RFG
(~35% moisture)
3.25 22% (wet) ~ 0.68
IFRF
2.5 MWth
wet RFG
(~ 26% moisture)
~ 2.20 48% (~41% wet) ~ 0.58
IHI 1.2 MWth wet RFG - ~34% (30%wet) -
CANMET 0.3 MWth wet RFG - 35% (dry) -
1
Molar ratio of the secondary comburent (oxidant)
2
% oxygen through the burner throat (volume dry basis)
3
MRFG and dMPFG are the mass flow rate of the recycled flue gas and product flue gas respectively
16

Recycle Rate and Oxygen Concentration
Universität ität Stuttgarttt t
a) b)
Flue Gas with Fly Ash
Oxygen
y O2 , mix
t adiabatic
Coal
Heat Output
Bottom Ash
Source: A. Kather, 2009
17

Factors affecting Recycle
Ratio
• Critical factors affecting the optimum
m
amount of recycled flue gas
• Burner and boiler design (heat transfer and flame
stability – oxygen distribution through burner)
• Air ingress
• Purity of oxygen from the ASU
• Coal type
• Level of moisture content in comburent
• Comburent (oxidant) temperature
18
18

Flame Description – Impact of Recycle Ratio
(Courtesy of IFRF)
Figure 3(a): normal air-fired operation Figure 3(b): O 2 -RFG flame with recycle ratio = 0.58
Figure 3(c): O 2 -RFG flame with recycle ratio = 0.76 Figure 3(d): O 2 -RFG flame with recycle ratio = 0.52
19

Coal Flame Photos:
Air Fired vs Oxy-Fired
(Courtesy of IHI)
Air mode(O 2 :21%)
Oxy mode(O 2 :21%) Oxy mode(O 2 :30%)
20
20

Coal Flame Photos:
Impact of Recycled Flue Gas
(Courtesy of IFRF)
Recycle Ratio = 0.58
(~ 0.61 include the CO2 to transport coal)
Recycle Ratio = 0.76
21
21

Effect of Different Oxygen Concentrations
(and Recycle Rates) on Flame Pattern
Universität ität Stuttgarttt t
Air
Oxyfuel
Oxyfuel
28% O 2 38% O 2
Recycle rate 77% Recycle rate 66%
Source: J. Smart, 2008
22

Ratio of Convective Heat Transfer Coefficient
(Courtesy of IFRF)
h1 ⎛ Re1
⎞ ⎛ Pr
=
h
⎜
⎟
⎜
0
Re
0 ⎠ ⎝ Pr
n
1
⎞
⎟
⎠
1
3
⎛ k
⎜
⎝ k
⎝ 0 0
1
⎞
⎟
⎠
Effect of Recycle Ratio on Convective heat transfer coefficient [IFRF APG1 Trials]
23
23

Radiative Heat Flux Measurements
(Courtesy of IFRF)
Ellipsoidal Radiometer
Results were also
obtained by:
• ANL-EERC
•CANMET
Data from Narrow Angle
Radiometer is necessary
for radiation modelling
development
Radiative Flux Using Ellipsoidal Radiometer in Air
(Baseline) and O 2 /RFG (Flames B with recycle ratio = 0.73
and Flame C with recycle ratio = 0.58) – IFRF APG2 Trials
Research in the past
decade has achieved
better understanding to eh
Radiation Principle of
oxyfuel boiler
24

Results: Radiative HT- South African coal – Dry
Recycle
m 2
Radiat tive Heat Flux kW/m
500
450
400
350
300
250
Furnace Heat Flux Measurements
South African coal, Oxyfuel (3% O 2 )
SAcoal/Air - 3% O2
Oxyfuel RR 65%
Oxyfuel RR 68%
Oxyfuel RR 70%
Oxyfuel RR 72%
Oxyfuel RR 75%
200
0 500 1000 1500 2000 2500 3000 3500
Axial Distance from Burner, mm
25

Normalised Convective & Radiative
heat flux – Russian Coal - Dry Recycle
tic
e
ed Adiabat
emperature
Normalise
Flame Te
Dry Oxyfuel Operation Normalised to Air Operation
Peak Radiation Flux, Convective heat transfer and calculated flame temperature
1.6
Russian coal
1.6
1.4
12 1.2
1
0.8
06 0.6
Measured Convective Heat
Transfer Coefficient i indicates 74%
Recycle is "Air-equivalent"
Normalised Flame Temperature (calculated)
Peak Normalised Heat Flux (measured)
Normalised Convective HTC (measured)
New Build Retrofit Avoid
Calculated dry oxyfuel adiabatic
flame temperatures are
equivalent to air at 69% recycle
Measured Peak Radiative
data indicates 74%
Recycle is "Airequivalent"
0.4
0.4
60% 65% 70% 75% 80%
Effective Recycle Ratio
1.4
12 1.2
1
0.8
06 0.6
e and
ux
ed Radiative
ctive Heat Flu
Normalise
Convec
26

Considerations in the Boiler Operation
O2 Purity and Air Ingress
(a.) Why not 99+% O2 Purity
(b.) Air Ingress… A Challenge for the Operator
27

Issue of Air Ingress (Air In-leakage)
Air Ingress in the boiler is a
fact of life!!!
1 st Large Scale Demonstration of
Oxy-Coal Combustion (35MWth)
– What Are the Lesson Learned...
28

Problem with Air Ingress
1 st Large Scale Oxy-Coal Combustion
Burner Test Experience - International Combustion Ltd.
30 MWth Low NOx burner
Because of Air Ingress the desired CO2
composition (only ~ 28% dry basis).
Air Ingress in boilers
approx. 3 % of flue gas flow for
a new conventional power plant
up to 10 % over the years for
power plants in use
29

CO 2 Recovery Depends On
Feed Composition
1
0.8
Recovery 0.6
0.4
0.2
0
0 0.2 0.4 0.6 0.8
Feed Composition
At -55°C C, 30 bar
30

NOx Emissions
We have quite a good confidence in
- We have quite a good confidence in
knowing the trend of these emissions

NOx Emissions
(Results from ANL-EERC and IFRF)
32
32

Results from IFRF study (APG4)
33

SO2 Emissions
- Highly dependent on how
sulphur is captured in ash...
- without the removal of SO2 in the secondary RFG, it should
noted that a maximum of ~30% reduction could be expected
(on mass per unit energy input basis)

SO2 Emissions
(Results from ANL-EERC and IFRF)
0.8
0.7
2 Emissions (lb/M MMBtu)
SO2
0.6
0.5
0.4
0.3
0.2
EERC‐ANL (Wet RFG)
EERC‐ANL (Dry RFG)
0.1
Air Fired Case
0
1.5 2 2.5 3 3.5 4
[CO2 + H2O]/[O2] Molar Ratio of Comburent
35
35

SO2 Emissions
(Results from IFRF)
36

Sulphur in ash
37
37

Fundamental question in attempt to
explain the reduction of SO2…
• Reduction of SO2 under oxy-coal combustion
conditions - Could this observations due to 2
competing phenomena in the furnace and in the
convective section
• High htemperature t sulfation of fthe ash h( (as proposed dby
Okazaki et. al.) - which could be in agreement base on
the data of IFRF (APG2 Trials).
• Sulfur capture in ash at convective section enhanced by
higher SO3 formation, higher deposition rate and lower
carbon in ash.
38
38

39
39

40
40

41
41

42
42

Results from IFRF study (APG2)
43
43

Issue of SO3
- The confirmation of the ANL results
as presented from the results of IVD
Stuttgart, ttgart IHI/Calide Project, Vattenfall,
Chalmers University.
- Nonetheless, there are still a lot of
,
confirmation to be done!!!

Oxy-Combustion: o KEY ISSUES
S
• SO3 issue is a big
missing link! (4 years
ago)
• ANL study (1985) have
indicated that SO3
formation is 3 to 5 times
greater as compared to
conventional air – firing
mode
• We need to know more
about the potential From Chemical Engineering Progress (Vol. 70)
operational issue.
http://www.ieagreen.org.uk 45
45

SO3 formation is increased in the presence
of firon oxide in the ash
Marrier and Dibbs (1974) Thermochmica Act (Vol. 8)
46
46

SO 2 captured along the convective part
(down to 450°C) by different inlet concentrations
500
KK_Captured RH_Captured LA_Captured EN_Captured
SO 2 captured
@ flue-g gas
path [ppm]
400
300
200
100
0
SO 2 injection increased
0 1000 2000 3000 4000
SO 2 measured at the end of radiative section [ppm]
Oxy-fuel 27 % O 2
47

IHI – Callide Project Results (SO2 Emissions)
IFRF (APG1 Trials) – Gottelborg coal
500
CoalA
CoalB
SO2,O xy m ode (mg/MJ)
400
300
200
100
CoalC
0.8
0.7
0.6
ANL-EERC Trials – Blk. Thunder coal
0
0 100 200 300 400 500
SO2,A ir m o de (m g/ M J )
SO2 Emissio ons (lb/MMBtu)
0.5
0.4
0.3
0.2
EERC‐ANL (Wet RFG)
0.1
EERC‐ANL (Dry RFG)
Air Fired Case
0
1.5 2 2.5 3 3.5 4
[CO2 + H2O]/[O2] Molar Ratio of Comburent

Would the capture of SO2 / SO3 in the ash
enhanced by lower carbon in ash
Marrier and Dibbs (1974) Thermochmica Act (Vol. 8)
E.ON UK Results at 26%O2
49
49

Emissions – SO 2
© 2004 E.ON 2012 年 3 月 29 日 , E.ON UK, Page 50

Ash Related Issue
Data from the trials taken by:
MBEL (Doosan Babcock), Air
Products, Ulster University
and Naples University (1995)
51

Summary SO2/SO3 and Sulphur
in Ash – (1)
• Capture of sulphur in ash at the furnace section is primarily due to
the high temperature direct sulphation mechanism as suggested
by Okazaki et. al. (2001) as shown in their experimental results.
This is pretty much in agreement to the in-flame SO2
measurements done by IFRF during their APG2 trials.
• Okazaki et. al. suggested that this is due to promotion of capture of sulphur
by CaO species and the inhibition of the decomposition of CaSO4
• This mechanism is further supported from the results of IVD Stuttgart (Maier
et. al.) and Imperial College (Wrigley et. al.) indicating the occurrence of both
carbonation and sulphation in the ash collected from oxy-coal combustion
trials. This could indicate that equilibrium reactions promoting the formation
of CaCO3 and CaSO4 are probably favoured (or highly enhanced) under CO2
rich environment.
• These results established the feasibility of using in-furnace SO2 reduction by
using Ca(OH)2 or CaO injection.
52

Summary SO2/SO3 and Sulphur
in Ash – (2)
• Additional sulphur capture in ash could also be
promoted by increased formation of SO3.
• It should be recognised that both results s from ANL-EERC Cand IVD
Stuttgart confirms that SO3 formation is higher (about 4-5 times – in
terms of mass SO3 emissions per unit energy input) as compared to
air fired case. However, it is not yet clear if level of recycled SO2 has
it impact to the level of SO3 formation.
• Capture of sulphur by this mechanism would occur along the flue gas
path (during the convective section) as shown in the results by IVD-
Stuttgart.
o Furthermore, IVD-Stuttgart results indicated that the higher the level of SO2 are
recycled , the capture efficiency of sulphur in ash is more efficient.
o Nonetheless, it should be noted that that this observation in sulphur capture
efficiency is coal dependent.
53

Summary SO2/SO3 and Sulphur
in Ash – (3)
• Results from Marrier and Dibbs (1974) further support the observations
made by IVD Sttuttgart:
• maximum conversion of SO2 to SO3 would occur around 700-800 o C.
• Capture of sulphur in ash could be dependent on the concentration of CaO and MgO
in the ash. (This could probably be one of the reasons why capture efficiency of
sulphur becomes coal dependent)
• Iron oxides could enhanced the formation of SO3 therefore promoting the capture of
sulphur in the ash at the convective section. (This could probably be one of the
reasons why capture efficiency of sulphur becomes coal dependent).
• Carbon in ash could diminish the efficiency in the capture of sulphur in ash. This is
supported by various studies indicating a lower carbon in ash during oxy-coal
combustion trials (IHI, IFRF, ANL-EERC) showed a lower SO2 emissions (i.e. higher
degree of sulphur capture in ash). A higher carbon in ash by E.ON UK experimental
results indicated a nearly similar SO2 emissions to the air fired case.
• Higher ash deposition rate under the wet RFG trials could also promote
higher sulphur capture in the convective section. This should be further
validated!
54

SO3 Emissions
(Results from ANL-EERC, IVD Stuttgart, Callide/IHI)
SO3 Concentra ation (ppm m)
20
18
16
14
12
10
8
6
4
ANL ‐ Air
IVD Stuttgart ‐ Air
Callide IHI ‐ Coal A ‐ Air
Callide IHI ‐ Coal B ‐ Air
ANL ‐ Oxy
IVD Stuttgart ‐ Oxy
Callide IHI ‐ Coal A ‐ Oxy
Callide IHI ‐ Coal B ‐ Oxy
2
0
0 250 500 750 1000 1250 1500 1750 2000 2250
SO2 Concentration ti (ppm)
55

My Background Analysis…
• SO2 to SO3 conversion will most likely to occur at the convective
section…
Marrier and Dibbs (1974) Thermochmica Act (Vol. 8)
56
56

Similar SO 3 Conversion Rate As Air Firing -
Economizer Outlet Measurements in BSF
Illinois Bituminous
Economizer Outlet t SO 3 results
North Dakota
Economizer Outlet t SO 3 results
SO3 ppm mv
300
250
200
150
100
50
Air
Oxy w/o SOx control
Oxy w/SOx control
3%
2%
1% Conversion
SO3 ppmv
100
75
50
25
Alstom 15MW th BSF
Lignite SO 3 Testing - Economizer Outlet
Air
Oxy w/o SOx control
Oxy hot FGR
Oxy w/SO3 spike
3%
2%
1% Conversion
0
0 5,000 10,000 15,000
SO2 ppmv
0
0 500 1,000 1,500 2,000 2,500 3,000 3,500
SO 2 ppmv
Similar SO2 to SO3 conversion rates
© ALSTOM 2011. All rights reserved. Information contained in this document is indicative only. No representation or warranty is given or should be relied on that it is complete or correct or will apply to any
particular project. This will depend on the technical and commercial circumstances. It is provided without liability and is subject to change without notice. Reproduction, use or disclosure to third parties, without
express written authority, is strictly prohibited.

Burner Development for Oxyfuel
Combustion
• Burners are critical to combustion, emissions,
and thermal efficiency / capacity of the utility
boilers
• Critical importance to burner development is a
full scale testing
• This is an important exercise to establish reference data
that could be used in the development and validation of
different modeling tools.
• This is also to gain experience in operating full scale
burner. (i.e. start up/shut down, flame stability, efficiency,
heat transfer, fouling and slagging, etc…).
58
58

Burner Development for Oxyfuel
Combustion
• Development of Full Scale Burner Testing
Programme could either be accomplished by:
• Retrofitting of Full Scale Burner Test Rigs
o B&W’s 30MWth CEDF Facility (Ohio, USA)
o Doosan Babcock’s 40MWth MBTF Facility (Renfrew, Scotland)
o Alstom ‘s 15MWth BSF Facility (Connecticut, USA)
• Testing in a Full Chain Oxyfuel CCS Pilot / Demo Plant
o Vattenfall’s Schwarze Pumpe Pilot Plant (Cottbus, Germany)
o CS Energy’s Callide Power Plant (Queensland, Australia)
o TOTAL’s Lacq Facility (Lacq, France)
o CIUDEN Demo Facility (El Bierzo, Spain)
59

Today... There are 3 Major Full Scale
PC Burner Testing Facilities Worldwide Retrofitted for Oxyfuel
• Babcock and Wilcox (B&W) • Doosan Babcock – • Alstom Power Plant Lab. –
30MWth CEDF
• Barberton, Ohio, USA
• Start of Operation: Oct. 2008
40MWth in 90MWth MBTF
• Renfrew, Scotland, UK
• Start of Operation: Jun. 2009
15MWth in 30MWth BSF
• Windsor, Connecticut, USA
• Start of Operation: Nov. 2009
• Wall Fired Burner
• Wall Fired Burner
• T-Fired Burner Development
Development
Development
Courtesy of Alstom, B&W and Doosan Babcock
60
60

OxyCoal 2 Demonstration of an Oxyfuel Combustion System
Officially opened on 24 th July 2009 Doosan Power Systems’ 40MW th OxyCoal
demonstration became the world’s largest demonstration of an oxyfuel combustion
system.
61
14 September 2011 | D W Sturgeon

OxyCoal 2 Demonstration of an Oxyfuel Combustion System
Safe and smooth transitions between air and oxyfuel operation were demonstrated,
with realistic CO 2 levels achieved (in excess of 75% v/v dry, and up to 85% v/v dry).
Oil
Air Firing
i
(TFGR,
PA, SA)
Secondary
Air to
Secondary
Flue Gas
Recycle
Transition
Oil
Air/Oxyfuel
Firing
(TFGR,
PA, SFGR)
Oil/Coal
Air/Oxyfuel
Firing
(TFGR,
PA, SFGR)
Coal
Air/Oxyfuel
Firing
(TFGR,
PA,
SFGR)
Primary Air
to Primary
Flue Gas
Recycle
Transition
Coal
Oxyfuel
Firing
(TFGR,
PFGR,
SFGR)
62
14 September 2011 | D W Sturgeon

OxyCoal 2 Demonstration of an Oxyfuel Combustion System
40MW th OxyCoal burner turndown proven from 100% load to 40% load.
40MW t
32MW t
24MW t
16MW t
20MW t
• Stable rooted flame maintained for all
loads down to 40% with coal ignition
within the burner throat/quarl.
• Comparable turndown to Doosan
Power Systems’ commercially
available air firing low NO X axial swirl
burners.
14 September 2011 | D W Sturgeon
63

View on Oxyfuel Pilot Plant
64 | Lars Strömberg, IEAGHG OCC2 Australia | 2011.09.12

Results until May 2011
Operating hours 14.200
Captured amount of CO2 11.500 t
CO 2 -removal rate > 93 %
CO 2 - purity > 99.7 %
• Stable oxyfuel operation
• All emission and safety values contained
• Interaction between all plant components
and subsystems validated
• Over 50 tests t with Boiler, ASU, CO2 plant
and all other components
• Plant availability very high
• Integration of a "cold DeNOx"
4 different burners tested
New tail end concepts commissioned
with good results
65 | Lars Strömberg, IEAGHG OCC2 Australia | 2011.09.12

Boiler and Burner
• Till now three burners tested (Jet-/spin-, pure spin burner)
• Igniting burner in main burner integrates
• Variable spinn during operation necessary
Results:
• Good ignition behavior
• High flame stability
• Emission values are kept for certain
Alstom-Burner Typ A and Typ B
1
Oxidantquerschnitt 1
3
Oxidantquerschnitt 2
1
2
5 6
4
3
Drall
1
5 6
2
4
3
Drall
Drall
2
4
5
Oxidantquerschnitt 3
Stauring
Staub- / Fördergas-
Querschnitt
HPE DS®-T Burner
6
Kernoxidant Querschnitt
Quelle: ALSTOM
66 | 2OCC, U.Burchhardt | 2011-09-13

Boiler (furnace) - Temperature Comparison (Front View)
Oxy 24% Oxy 28% Oxy 32% Oxy 36% Air (21%)
• The gas temperatures increases with increased O2 in oxidant as expected
• The temperature levels for air case corresponds to OXY28
67 | 2OCC, U.Burchhardt | 2011-09-13

30 MW th Oxy-Combustion Pilot Plant
Burner Design Type A and B
Burner Type A
Burner Type B
Oxy-Combustion Testing in 30MWth Pilot Plant Schwarze Pumpe - IEA-OCC2 Yeppoon, Australia - Frank Kluger - 14 Sep 2011 - P 68
© ALSTOM 2011. All rights reserved. Information contained in this document is indicative only. No representation or warranty is given or should be relied on that it is complete or correct or will apply to any
particular project. This will depend on the technical and commercial circumstances. It is provided without liability and is subject to change without notice. Reproduction, use or disclosure to third parties, without
express written authority, is strictly prohibited.

DST Burner
for indirect firing
‣ Hours installed:
‣ Oxyfuel operation:
‣ Air operation:
10.200 h (19 th of April – 16 th of June)
4.760 h
1.250 h
2nd International Oxyfuel Combustion Conference, 12th-16th September 2011, Yeppoon, Australia © Hitachi Power Europe GmbH 69

DST burner
2nd International Oxyfuel Combustion Conference, 12th-16th September 2011, Yeppoon, Australia © Hitachi Power Europe GmbH 70

Premixed / hybrid mode
Premixed mode
DST burner
Hybrid mode
DST burner
M
M
M
M
M
M
Flue gas
Flue gas + O 2
Flue gas
M
O 2
O
O 2 71
O 2
M
O 2
M
2nd International Oxyfuel Combustion Conference, 12th-16th September 2011, Yeppoon, Australia
© Hitachi Power Europe GmbH

Oxyfuel operation - Oxyfuel flame example
Heat input: 27 MW th
O 2 in oxydant: 32 % by vol. (wet)
NO x : 416 mg/m³ = 013 0.13 kg/MWh
2nd International Oxyfuel Combustion Conference, 12th-16th September 2011, Yeppoon, Australia © Hitachi Power Europe GmbH 72

CS Energy/IHI Burner Testing Programme at
Callide A Power Stationti
• Callide A Project – would
be the world’s 1 st oxyfuel
retrofitted power station.
• First oxyfuel pilot plant that
will actually produce
electricity.
• Installation ti of 2 new Wall
Fired Burners
• A unique position to provide
information related to the
burner – burner interaction
Courtesy of CS Energy, IHI
73
73

Thank you
• Email:
• Website:
stanley.santos@ieaghg.org
http://www.ieaghg.org
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