Challenges in Understanding the Fate of Mercury during Oxyfuel Combustion

Stanley SantosIEA Greenhouse Gas R&D Programme

Cheltenham, UK

Email: stanley.santos@ieaghg.org

MEC7 WorkshopDLCS, Strathclyde University

18th June 2010

IEA Greenhouse Gas R&D Programme• A collaborative research programme founded in 1991• We are the sister organisation of IEA Clean Coal Ce ntre• Aim: Provide members with definitive information on

the role that technology can play in reducing greenhouse gas emissions .

2

greenhouse gas emissions .• Producing information that is:

� Objective, trustworthy, independent� Policy relevant but NOT policy prescriptive� Reviewed by external Expert Reviewers� Subject to review of policy implications by Members

• Funding approx 3 million €/year

Contracting Parties and Sponsors

3

Acknowledgement• IEA Clean Coal Centre

• Lesley Sloss• Robert Davidson

• Vattenfall R&D AB• Marie Anheden• Jinying Yan

• E.On Engineering UK

• Doosan Babcock• Jacqueline Gibson• Connie Ellul• Bhupesh Dungel

• Stuttgart University• Jorge Maier

• Air Products

4

• E.On Engineering UK• Robin Iron

• Utah University• Prof. Jost Wendt

• Leeds University• Maryam Gharebaghi• Richard Porter

• IHI• Toshihiko Yamada

• Air Products• Vince White

• Air Liquide• Jean Pierre Tranier

• Praxair• Minish Shah

Special Workshop on Oxyfuel Combustion

SO2/SO3/Hg/Corossion Issues in Oxyfuel Combustion Boiler

London, UK25th – 26th January 2011

Email: stanley.santos@ieaghg.org

5

Area of Discussions:1) Fundamental Experimental work on SO2/SO3/Hg emission

from oxyfuel combustion boiler2) SO2/SO3/Hg/Cl measurement techniques under oxyfuel

combustion conditions3) Impact of Sulphur species to the Flue Gas Processing Units

(ESP/FF, FGD, Direct Contact Cooler, Wet Scrubbers)4) Boiler Corrosion issue – under oxyfuel combustion conditions5) Modelling work on SO2/SO3/Hg from oxyfuel boilers6) Experience from large scale demonstration/pilot plant projects

Presentation Outline

• Objective of this Presentation• Brief Introduction

• Oxyfuel combustion of power plant with CO2capture

6

• Why we need to understand the fate of Hg during combustion?

• Review of Literature – Where are we in our understanding of fate of Hg during oxyfuel combustion.

• Where are the challenges.

Objectives of this Presentation

• To provide awareness the impact / risk of ignoring Hg in any Oxy-Coal Combustion Power Plant with CO 2 Capture Power Plant

• To initiate discussion on the issue of Mercury in

77

• To initiate discussion on the issue of Mercury in Oxy-Coal Combustion Power Plant with CO 2Capture

• To initiate a review on the different factors to reconsider on the design of coal power plant in the perspective of Hg.

Oxy-PC Combustion Fired Power Plants with CO 2 Capture

8

with CO 2 Capture

Oxy-Coal Combustion Power Plant with CCS…

9

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

10

Alstom Schwarze Pumpe 2008 30MWth Lignite

Hitachi Babcock Schwarze Pumpe 2010 30MWth Lignite

IHI Callide 2011 30MWe

Alstom / AL Lacq 2009 30MWth Gas/Oil?

CIUDEN El Bierzo CFB Facility 2011 30MWth Coal

El Bierzo PC Facility 2010 20MWth Coal

Coal

CIUDEN

Brindisi Test Facility 2012 48MWth CoalENEL HP Oxyfuel

2008

World’s FIRST 30 MWt

full chain demonstration

at Schwarze Pumpe Pilot Plant

2009 – Lacq – World’s

first 30MWt

retrofitted Oxy-NG

boiler2011 – CIUDEN –

World’s first 30MWt

Oxy-CFB Pilot Plant

2011 – Callide –

World’s first 30MWe

retrofitted Oxy-coal

power plant

By 2014-2018

Demonstration of

50– 300MWe full

scale power plant.

Target :

“Commercialised by 2020”

Vattenfall - Janschwalde (PC -250MWe)

KEPCO/KOSEP - Yongdong (PC - 100MWe)

Endesa/CIUDEN - El Bierzo (CFB - 300MWe)

1980’s

ANL/Battelle/EERC completed the first

industrial scale pilot plant

1990 - 1995

EC Joule Thermie Project

- IFRF / Doosan Babcock / Int’l Combustion

NEDO / IHI / JCoal Project

First large scale 35MWt

Oxy-Coal Burner Retrofit

Test done by

International Combustion

1998 – 2001

CANMET

US DOE Project / B&W / Air Liquide

2003 - 2005

Vattenfall (ENCAP ++)

CS Energy / IHI Callide Project

B&W CEDF 2008 30MWth Coal

Alstom Alstom CE 2010 15MWth Coal

Doosan Babcock DBEL - MBTF 2009 40MWth Coal

2007

B&W CEDF (30MWt)

large scale burner testing started

Updated by S. Santos (17/06/2010)

at Schwarze Pumpe Pilot Plant

By the end of 2010/2011,

Users (i.e. Power Plant Operators)

will have 6 burner manufacturers

fully demonstrating “Utility Size

Large Scale Burners” which should

give a high level of confidence

toward demonstration

Today... There are 3 Major Full Scale PC Burner Testing Facilities Worldwide Retrofitted for Oxyfuel

12

• Babcock and Wilcox (B&W)30MWth CEDF

• Barberton, Ohio, USA

• Start of Operation: Oct. 2008

• Wall Fired Burner Development

12

• Doosan Babcock –40MWth in 90MWth MBTF

• Renfrew, Scotland, UK

• Start of Operation: Jun. 2009

• Wall Fired Burner Development

• Alstom Power Plant Lab. –15MWth in 30MWth BSF

• Windsor, Connecticut, USA

• Start of Operation: Nov. 2009

• T-Fired Burner Development

Courtesy of Alstom, B&W and Doosan Babcock

Jänschwalde demonstration plant – view from south east

PCC

Cooling waterpump

CO2-compression

NH3-storage

© Vattenfall AB 14

Fuel feeding

Lignitedryer

Oxyfuelboiler

ASU

Flue gas cleaning

CO2-compressionPreparation and cleaning ofLignite condensate

PCC

CO2-transport

CO2-compression

Why it is important to understand the fate of mercury during Oxyfuel Combustion?

Why Mercury is an operational issue to Oxyfuel Combustion Power Plant?

15

Oxyfuel Combustion Power Plant?

Case 1: Moomba Gas PlantCase 2: Skikda Gas Processing Plant

Case 1: Moomba Gas Plant Accident caused by Mercury

• Moomba Gas Processing Plant, owned by Santos, is th e main supplier of natural gas to South Australia and New South Wales• Liquids separated from raw natural gas via 2 trains of LRP (Liquids

Recovery Plant)•

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• Liquids (condensate and LPG) sent to Port Bonython for export (about 650Km south of Moomba)

• A New Year BANG! About 02.43 in the morning, 1st January 2004 – an explosion & fire occurred at Trai n A of the LRP section.• The fire incident also damaged Train B.

• Effect: liquids production interrupted for 8 months

Failure Location

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• Failure occurred at the base (6 o’clock) of the gas nozzle• Evidence of de-lamination consistent with Liquid Me tal

Embrittlement (LME) caused by mercury in contact wi th aluminium

Case 2: Skikda Gas Processing Plant Accident• Skikda Gas Processing Plant is owned by Sonatrach i n

Algeria. • About 18.40 on 19 th January 2004 (just about 3 weeks

after Moomba Gas Processing incident) , an explosion occurred in Train “40”.

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• Consequence:• 3 out of the 6 NG liquefaction trains were destroyed and 2, which

were not operating at the time, were damaged. The administration building and the maintenance workshop, and other buildings, were completely destroyed.

• Sadly, 27 person killed and 80 people injured.• Adjacent oil refinery and power plant were shut down due to the blast

for at least a month.

18

Skikda Gas Processing Accident

19

Incident Report• The Report concludes that the explosion was the

consequence of a catastrophic failure in one of the cold boxes of Unit “40”, which led to a vapour cloud explosion of either LNG or refrigerant . The most probable source of ignition was the boiler at the north end of Unit “4 0”.

• Although (unlike the Moomba Gas Plant incident) – the report

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• Although (unlike the Moomba Gas Plant incident) – the report noted that it is not absolutely proven if Liquid Me tal Embrittlement is the main cause of the failure – non etheless, it was accepted that this was the most likely proba ble cause of the failure.

• Train “40” is the only NG Liquefaction train that d oesn’t have mercury removal system!

Discussion Points

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Discussion Points

CO2 Compression and Purification System –Inerts removal and compression to 110 bar

Flue Gas Expander

Aluminium plate/fin exchangerFlue GasHeater

Flue Gas Vent

1.1 bar20°C

25% CO275% inerts

-55°C

22

Driers

30 bar Raw CO2Saturated 30°C

76% CO2 24% Inerts

CO2 product110 bar

96% CO24% Inerts-60°C dp

Statement of Fact:

• For oxyfuel combustion – Mercury is not an environmental issue alone but also an operational issue particularly to the CO 2processing unit.

23

processing unit.• The issue of Mercury to oxyfuel

combustion is not about concentration –but it is about where Mercury could accumulate within the CO 2 processing unit!

23

Discussion Points(Oxyfuel Boiler)

Where we are in the understanding of:

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Where we are in the understanding of:• NOx Chemistry during combustion• SO2/SO3/Dew Point• Chlorine issue (Halogen issue)• Carbon in Ash• Brief review of some results presented regarding Hg under oxyfuel condition

Item Combustion with air Combustion with oxygen

Windbox O2 ２１％２１％２１％２１％ ２１～３０％２１～３０％２１～３０％２１～３０％

N2 ７９％７９％７９％７９％ （０）～１０％（０）～１０％（０）～１０％（０）～１０％

CO2 ００００% ４０～５０％４０～５０％４０～５０％４０～５０％

H2O Small １０～２０％１０～２０％１０～２０％１０～２０％

Coal Combustion under CO 2 Atmosphere

Others －－－－ NOx、SO2・・・

Flue gas O2 ３～４％３～４％３～４％３～４％ ３～４％３～４％３～４％３～４％

N2 ７０～７５％７０～７５％７０～７５％７０～７５％ （０）～１０％（０）～１０％（０）～１０％（０）～１０％

CO2 １２～１４％１２～１４％１２～１４％１２～１４％ ６０～７０％６０～７０％６０～７０％６０～７０％

H2O １０～１５％１０～１５％１０～１５％１０～１５％ ２０～２５％２０～２５％２０～２５％２０～２５％

Others NOx、SO2・・・ NOx、SO2・・・

（Wet％％％％ base））））

NOx Emissions

26

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

NOx Results from IFRF study (APG4)

27

SO2 Emissions

- Highly dependent on how

28

- Highly dependent on how sulphur is captured in ash...

- without the removal of SO 2 in the secondary RFG , it should noted that about ~30% reduction could be achieved ( on mass per unit energy input basis – especially for bitumi nous coal)

SO2 Emissions(Results from IFRF)

2929

SO3 Emissions(Results from ANL-EERC, IVD Stuttgart, Callide/IHI Aiolo)

10

12

14

16

18

20

Con

cent

ratio

n (p

pm)

ANL - Air ANL - Oxy

IVD Stuttgart - Air IVD Stuttgart - Oxy

Callide IHI - Coal A - Air Callide IHI - Coal A - Oxy

Callide IHI - Coal B - Air Callide IHI - Coal B - Oxy

30

0

2

4

6

8

10

0 250 500 750 1000 1250 1500 1750 2000 2250

SO

3 C

once

ntra

tion

(ppm

)

SO2 Concentration (ppm)

Correlation of SO 3-Moisture and Acid Dew Point(Result from Stuttgart University – IFK)

120

130

140

150

160S

äure

taup

unkt

stem

pera

tur [

°C] .

Oxyfuel

Aci

d de

w p

oint

tem

pera

ture

31

80

90

100

110

120

0 10 20 30 40

Wasserdampfkonzentration im Rauchgas [Vol. %]

Säu

reta

upun

ktst

empe

ratu

r [°C

] .

0,5 ppm SO3 1,0 ppm

2,0 ppm 5,0 ppm

10,0 ppm

Luft

Moisture content in flue gas

Aci

d de

w p

oint

tem

pera

ture

air

SO2 captured along the convective part(down to 450°C) by different inlet concentrations

Coal Type

Iron Content in the Ash

“KK” ~2-3%“KK” ~2-3%

“EN” ~17-18%

“LA” ~22-23%

“RH” ~16-17%

Chlorine / Bromine Chemistry

- This could be a big challenge to Oxyfuel Combustion because we hardly know anything about it under oxyfuel combustion condition.

33

about it under oxyfuel combustion condition.

- But ... What we currently know shows the possible impact of Chlorine and Sulphur to boiler corrosion.

CORROSION - Low-S/Low-Cl

El Cerrejon Oxy-Fuel

1.00E-10

1.00E-09

95%

ile P

arab

olic

Rat

e (c

m2s-

1 )

T22

T91

Seite 34Thema Datum Bereich

1.00E-14

1.00E-13

1.00E-12

1.00E-11

400 450 500 550 600 650 700

Temperature (oC)

95%

ile P

arab

olic

Rat

e (c

m

E1250

TP347HFG

HR3C

San25

IN740

CORROSION - High-S/High-Cl

Thoresby Oxy-Fuel

1.00E-10

1.00E-09

95%

ile P

arab

olic

Rat

e (c

m2s-

1 )

T22

T91

Seite 35Thema Datum Bereich

1.00E-14

1.00E-13

1.00E-12

1.00E-11

400 450 500 550 600 650 700

Temperature (oC)

95%

ile P

arab

olic

Rat

e (c

m

T91

E1250

TP347HFG

HR3C

San25

IN740

Addition of Calcium Chloride or Calcium Bromide to enhance oxidation of Hg may probably be a none starter under oxyfuel combustion conditions!!!

36

I could be a “villain” to a lot of commercial interests to this type of Hg reduction control technology!

But will the addition of other Calcium/Magnesium compounds enhance Hg removal???

Carbon in Ash

- This could be dependent to the burner design and combustion regime.

37

and combustion regime.

- It is expected that a lower Carbon in Ash during oxyfuel combustion conditions

Would the capture of SO 2 / SO3 in the ash enhanced by lower carbon in ash?Marrier and Dibbs (1974) Thermochimica Act (Vol. 8)

E.ON UK Results at 26%O2

38

38

Review of Literature

- Assessing all the published worked relevant to

39

- Assessing all the published worked relevant to Mercury and oxyfuel combustion

- Aim: My attempt to establish what we know...

Mercury

Speciation

• Hg measured by on-line analyzer• Hg data taken when firing lignite• Hg in flue gas (air firing) was ≈ 13.5µg/m 3• Hg concentration in flue gas increase in oxy mode

corresponded to removal of N 2. • Oxidized (ionic) Hg increased from 25% to 30%

© 2009 Babcock & Wilcox Power Generation Group, Inc. All rights reserved.© 2009 Babcock & Wilcox Power Generation Group, Inc. All rights reserved. .40

• Oxidized (ionic) Hg increased from 25% to 30% � Increases removal (less elemental Hg)

• Oxidized Hg removed in WFGD

CONCLUSIONS:

1. Hg oxidation may improve with oxycombustion2. Hg removal is expected to be the same as for air firing

Experimental Results from Guo et. al. (2009)Thermal Degradation of 3 Chinese Coal

41

Suriyawong et. al. (2005)

42

List of Literature• Gharebaghi, M., Goh, B., Porter, R.T.J., Pourkashan ian, M. and Williams, A.. (2009). Assessment

of Fate of Mercury in Oxy-coal Combustion. 1st In ternational Oxyfuel Combustion Conference (OCC1). Cottbus, Germany. (8-11 September 2009). I EA Greenhouse Gas R&D Programme.

• Gharebaghi, M., Hughes, K.J., Porter, R.T.J., Pourk ashanian, M. and Williams, A.. (2010). Mercury Speciation in Air- and Oxy-Coal Combustion: A Modell ing Approach. 33rd International Symposium on Combustion. Beijing, China.

• Guo, S., Yang, J., Liu, Z., and Xiao, Y.. (2009). Behaviour of Mercury Release During Thermal Decomposition of Coals. Korean Journal of Chemical Engineering. Vol. 26, pp. 560 -563.

43

Decomposition of Coals. Korean Journal of Chemical Engineering. Vol. 26, pp. 560 -563.

• McDonald D.K., DeVault D., Tranier J.P., Perrin N. (2009). Oxyfuel Process Developments Leading to Demonstration Plant Design. 1st International Ox yfuel Combustion Conference (OCC1). Cottbus, Germany. (8-11 September 2009). IEA Greenh ouse Gas R&D Programme.

• Pavlish, J.H., Hamre, L.L. and Zhuang, Y.. (2010). Mercury Control Technologies for Coal Combustion and Gasifications Systems. Fuel. (Vol. 8 9) pp. 838-847.

• Santos, S.O. (2006). Mercury (Hg) in Oxy-Coal Fired Power Plant with CO2 Capture -What is the Real Score? 3rd IEAGHG International Oxyfuel Combu stion Research Network Workshop. Yokohama, Japan. (5-6 March 2008).

•

List of Literature

• Sethi V., Omar K., Martin P., Barton T., Krishnamur thy K. (2007). Oxy-Combustion Versus Air-Blown Combustion of Coals. in “The Power of Coal.” The Proceedings of the 32nd International Technical Conference on Coal Utilization & Fuel Sys tems. Clearwater, FL, USA, 10-15 Jun 2007.

•• Suriyawong A., Gamble M., Lee M.H., Axelbaum R., Bi swas P. (2006). Submicrometer Particle

Formation and Mercury Speciation under O 2-CO2 Coal Combustion. Energy and Fuels. (Vol. 20), pp. 2357-2363.

•• Suriyawong A., Gamble M., Lee M.H., Axelbaum R., Bi swas, P. (2005). Submicrometer Particle

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• Suriyawong A., Gamble M., Lee M.H., Axelbaum R., Bi swas, P. (2005). Submicrometer Particle Formation and Mercury Speciation under Oxygen-Carbo n Dioxide Coal Combustion. Proceedings, 22 nd Annual Pittsburgh Coal Conference, Pittsburgh, PA, USA, 12-15 Sep 2005. Pittsburgh, PA, USA, Pittsburgh Coal Conference, pa per 275, 10 pp (2005) CD-ROM

•• Wall T., Liu Y., Spero C., Elliott L., Khare S., Ra thnam R., Zeenathal F., Moghtaderi B., Buhre B.,

Sheng C., Gupta R., Yamada T., Makino K. and Yu J. (2009). An Overview on Oxyfuel Coal Combustion - State of the Art Research and Technolo gy Development. Chemical Engineering Research and Design (Vol. 87). pp. 1003-1016.

Discussion Points

45

Discussion Points(CO2 Processing Unit)

CO2 Compression and Purification System –Inerts removal and compression to 110 bar

Flue Gas Expander

Aluminium plate/fin exchangerFlue GasHeater

Flue Gas Vent

1.1 bar20°C

25% CO275% inerts

-55°C

46

Driers

30 bar Raw CO2Saturated 30°C

76% CO2 24% Inerts

CO2 product110 bar

96% CO24% Inerts-60°C dp

NOx SO2 Reactions in the CO2Compression System� We realised that SO 2, NOx and Hg can be removed in the CO 2

compression process, in the presence of water and o xygen.

� SO2 is converted to Sulphuric Acid, NO 2 converted to Nitric Acid:

– NO + ½ O2 = NO2 (1) Slow– 2 NO2 = N2O4 (2) Fast– 2 NO2 + H2O = HNO2 + HNO3 (3) Slow

47

– 2 NO2 + H2O = HNO2 + HNO3 (3) Slow– 3 HNO2 = HNO3 + 2 NO + H2O (4) Fast– NO2 + SO2 = NO + SO3 (5) Fast– SO3 + H2O = H2SO4 (6) Fast

� Rate increases with Pressure to the 3 rd power– only feasible at elevated pressure

� No Nitric Acid is formed until all the SO 2 is converted

� Pressure, reactor design and residence times, are i mportant.

CO2 Compression and Purification System –Removal of SO2, NOx and Hg

1.02 bar 30°C67% CO28% H2O25% InertsSOx NOx

30 bar to DriersSaturated 30°C76% CO224% Inerts

� SO2 removal: 100% NOx removal: 90-99%

BFW15 bar

30 bar

Water

48

NOx

Dilute H 2SO4 HNO3

Hg

BFW

Condensate

cw

30 bar

cwcw

Dilute HNO 3

NG Industry Practice

• Activated Carbon bed is generally employed. This is expected to be applied to oxy-combustion oxy-PC as well.

• It is important to be aware

50

• It is important to be aware with regard to short term performance drop of the activated carbon bed during shut down or process upset.

• Competing reaction of Hg and Sulphur species

CO2 Compression and Purification System –Inerts removal and compression to 110 bar

Flue Gas Expander

Aluminium plate/fin exchangerFlue GasHeater

Flue Gas Vent

1.1 bar20°C

25% CO275% inerts

-55°C

51

Driers

30 bar Raw CO2Saturated 30°C

76% CO2 24% Inerts

CO2 product110 bar

96% CO24% Inerts-60°C dp

What is the Feasibility and Effectiveness of Cold Trapping of Hg as final polishing process?(Figure from US Patent 4982050)

52

• Hg is heavier than the gas at temperature colder than -10 oC (solid at -40 oC)

Summary and Conclusions

• For any oxy-combustion process, the removal of mercury from the CO 2 rich flue gas is a necessary to protect key components in the CO 2 clean up and

53

components in the CO 2 clean up and processing unit.

• Damage cause by Mercury to any aluminium based equipment is a Random Event!!!

53

Understanding Failure Mechanisms• Statement from ALPEMA:

In general, mercury will not react with aluminium u nless it is allowed to exist in contact with the heat exchanger in its liquid state and there is water present . If these conditions exist within a heat exchanger, then mercury contamination can resu lt in problems. This attack is most severe when coupled w ith another corrosion process.

54

• Currently, the common practice of NG Processing means reducing the mercury to less than 0.01 µg/Nm3.

• QUESTION: Is the 0.01 µg/Nm3 to be used as well in the oxy-coal combustion power plant?

54

Summary and Conclusions

• What is the speciation of Hg in an oxy-coal combustion cases?• Together with this challenge is how we measure

the speciation under oxyfuel combustion

55

the speciation under oxyfuel combustion condition?

• How we deal with the impact of:• Higher concentration of NOx, SOx, HCl, HBr,

CO2, etc...

55

Role of Chlorine and its Chemistry• What is the role of Coal Chlorine and its

Chemistry to the heterogeneous and gas phase oxidation of Hg under oxyfuel condition.

56

condition.

• SO2(g) + Cl 2(g) + H2O(g) ↔ 2HCl(g) + SO3(g)

Impact of SO 3 on Hg Removal Efficiencyof the Activated Carbon

Air Fired Case (CODEN Study) Oxy Fired Case

57

Mercury Management in the CO2 Processing Plant

• I don’t see any technical barrier in removing Hg. This has been done in LNG industry. The consideration of cost is the main question!

58

• There are 3 levels where Hg (both elemental and ionic) could be captured in the CO 2 processing plant.• Compression stage• Moisture Removal stage• Activated Carbon Guard bed

59

CS Energy/IHI Burner Testing Programme at Callide A Power Station

• Callide A Project – would be the world’s 1 st oxyfuel retrofitted power station. (Would be the largest demonstration of the technology by 2011!)

• First oxyfuel pilot plant that will actually produce electricity.

• Installation of new IHI 2x ~30MWth Wall Fired Burners (with operation of 4 burners at full load)

60

load)o A unique position to provide information related to

the burner – burner interaction

• Project Scope (4 years operation):o Oxygen plant (nominal 2 x 330 tpd ASUs)o Boiler refurbishment and oxy-fuel retrofit (1 x 30

MWe Unit)o CO2 compression & purification (75 tpd process

plant from a 20% side stream)o Road transport and geological storage (~ 30 tpd

liquid CO2)Courtesy of CS Energy, IHI

Interest to receive updates - Please Register at:

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Conference Dates:12th Sept. 2011 Asia Pacific Programme - Oxyfuel Working Group Capacity Building Course

61

12th Sept. 2011 Asia Pacific Programme - Oxyfuel Working Group Capacity Building Course12th–15th Sept. 2011 2nd Oxyfuel Combustion Conference16th Sept. 2011 Facility Visit to Callide Power Station

Dates to Remember:15th Sept. 2010 Call for papers opens15th Dec. 2010 Deadline for Abstract Submission15th Feb. 2011 Conference Registration opens15th Apr. 2011 Notification of Acceptance for Oral / Pos ter Presentations15th May 2011 Early Bird Registration Deadline12th – 16th Sept. 2011 2nd International Oxyfuel Combustion Conference