Diglycolamine® Solvent Quality Improvement with Thermal Reclaiming

Don DaughtonSuncor Energy Inc.

Bob VerobaHuntsman Corporation

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OutlinePlant OverviewOperations Prior to Thermal ReclaimingMerchant ReclaimingThermal Reclaimer DesignOperations After Thermal ReclaimerInstallationConclusionsRecommendations

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Suncor Plant Location

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Oilsands Mining/Extraction

5

Millennium Upgrader

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Plant OverviewMillennium Amine Unit (Plant 53) Start up in 2001Main Fuel Gas Absorber, Primarily Coker Gas, 77 MMSCFD, 15% H2S, 1% CO23 Hydrotreater Absorbers, 540 MMSCFD Total, 0.4 to 1.8% H2S, no CO21 Liquid C4 Treater, 30 gpm, 100 ppm H2SCommon Regenerator for all AbsorbersTotal Circulation Rate 2500 gpm DGA® at 35 to 40 weight percent

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Plant OverviewDEA For Original Plant DesignDGA® Chosen to Achieve Future Expansion Capacity, Fuel Gas Total Sulfur at Low Operating PressureExisting DEA Unit Has High HSS and CO2/COS DegradationExpected Need to Reclaim - Tie in Points Added

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Operations Prior to Thermal ReclaimerAmine Degradation Did OccurBHEEU Formation at 2 WT%/Month due to COS Removal, Maximum Over 20 WT%Heat Stable Salts Were < 2 WT%No Significant Operating Problems Due to BHEEUMerchant Reclaiming Used to Maintain Amine Quality

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BHEEU HistorySuncor BHEEU

-5

0

5

10

15

20

25

30

35

April 19,2001

November5, 2001

May 24,2002

December10, 2002

June 28,2003

January 14,2004

August 1,2004

February17, 2005

September5, 2005

March 24,2006

October 10,2006

April 28,2007

Date

Wei

ght P

erce

nt

BHEEU

Reclaimer Start upFebruary 2006

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Heat Stable Salt HistorySuncor Heat Stable Salts

0

0.5

1

1.5

2

2.5

3

3.5

4

4.5

April 19,2001

November5, 2001

May 24,2002

December10, 2002

June 28,2003

January 14,2004

August 1,2004

February17, 2005

September5, 2005

March 24,2006

October 10,2006

April 28,2007

Date

HSS

WT%

HSS

Reclaimer Start upFebruary 2006

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Merchant ReclaimingMerchant Reclaiming Needed 2 Times per YearBHEEU Content Range 10 to 25 Weight %Minimal BHEEU Conversion50 MT of 80% Nitrogen Waste per Reclaim –Environmental Concern Expansion Capacity Needed 50 Weight % DGA®

High Viscosity Issues at High Amine WT%Permanent Operation With < 10% Degradation Needed

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Thermal Reclaimer DesignBHEEU Reversed/Recovered In Thermal Reclaimerat 360oF2*DGA® + (CO2 or COS)<-> BHEEU + (H2O or H2S)2 Control Loops

Temperature Control at 360oF Using Water FeedLevel Control With Lean Amine Feed

Vapor Returned to Regenerator Reclaimer Heat Input = Regenerator Reboiler Reduction

300 Day Cycle Time, Depending on Solids/Non-Volatile Accumulation

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Thermal Reclaimer DesignDesign for Current DGA® Unit (Plant 53) and Future Plant 68Maximum Heat Duty 41 MMBtu/hrMaximum Amine Feed Rate 49 gpm Total

27 gpm Plant 53 and 22 gpm Plant 68 (2008 Start up)

12’ ID X 24’ T/T, 15,000 Gallon CapacityTarget BHEEU 3 WT%

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Suncor Reclaimer Schematic

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Operations After Thermal ReclaimerInstallation

Start Up February, 2006Steam Trap/Condensate Return ProblemsTemperature Controller Calibration IssuesLevel Control Range Conflicts

BHEEU Reduced from 17 WT% to 3 WT% in 3 MonthsAmine Consumption Reduced Due to Conversion of BHEEU to DGA®

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BHEEU After Reclaimer Start upBHEEU After Reclaimer

-5

0

5

10

15

20

December 14,2005

February 2,2006

March 24, 2006 May 13, 2006 July 2, 2006 August 21,2006

October 10,2006

November 29,2006

January 18,2007

Date

Wei

ght %

BHEEU

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Operations After Thermal ReclaimerInstallation

Particulate Filter Replacement Reduced by 50%2:1 Length to Diameter Ratio was Effective in Eliminating Carryover Out of ReclaimerRegenerator Reboiler Temperature Reduced Due to Higher Water Content in Amine SolutionFirst Reclaim Cycle was 9 Months

Steam Coil Leak Was Found – Vibration Was Main Cause, Possibly Due to Changes to Inlet Distributor

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Amine Feed Rate To ReclaimerAmine Feed to Reclaimer

0

5

10

15

20

25

30

35

40

45

22/0

2/20

06

08/0

3/20

06

22/0

3/20

06

05/0

4/20

06

19/0

4/20

06

03/0

5/20

06

17/0

5/20

06

31/0

5/20

06

14/0

6/20

06

28/0

6/20

06

12/0

7/20

06

26/0

7/20

06

09/0

8/20

06

23/0

8/20

06

06/0

9/20

06

20/0

9/20

06

04/1

0/20

06

18/1

0/20

06

01/1

1/20

06

Date

Flow

(USG

PM)

USGPM

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Steam Rate To ReclaimerReclaimer Steam Rate

0

2000

4000

6000

8000

10000

12000

14000

16000

14/12/2005 02/02/2006 24/03/2006 13/05/2006 02/07/2006 21/08/2006 10/10/2006 29/11/2006

Date

Stea

m (l

b/hr

)

Steam (lb/hr)

22

Reboiler TemperatureReboiler Temperature

245

250

255

260

265

270

275

280

05/09/2005

25/10/2005

14/12/2005

02/02/2006

24/03/2006

13/05/2006

02/07/2006

21/08/2006

10/10/2006

29/11/2006

Date

Deg

rees

F

Reboiler Temperature (F)

Reclaimer Start upFebruary 2006

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ConclusionsBHEEU and Degradation Targets Met with New Thermal ReclaimerIncrease in Amine Strength is Now Possible for Capacity IncreaseWaste Volume and Nitrogen Content Has Been ReducedAmine Losses ReducedMerchant Reclaiming Costs Eliminated

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RecommendationsReclaimer Design for Future Voyageur Expansion Project Will Be Based on Plant 53/68 DesignImprovements to Level and Temperature Indication Will Be ImplementedCondensate Drum Should be Considered for Future DesignsVibration Analysis and Inlet Design Are Important in Future Designs2:1 L:D Ratio is Effective in Reducing Liquid Carryover