Presentation by Ron Munson, Global CCS Institute at the 2015 CCUS Workshop on CO2 Storage, January 22 at the University of Sonora, Hermosillo

1. Carbon Capture
Ron Munson
Global CCS Institute
INTRODUCTION TO CAPTURE, USE AND GEOLOGICAL STORAGE OF CO2
January 22-23 2015
University of Sonora, Hermosillo
SUPPORTED BY:

2. Presentation Overview
SUPPORTED BY:
• Background
• Solvent-Based Capture
Post-Combustion
Pre-Combustion
• Sorbent-Based Capture
• Oxy-Combustion
• Industrial CCS
• Case Study
• Innovation

3. Evolution of Industrial Gas Processing
SUPPORTED BY:
1900s 1920s 1940s 1960s 1980s 2000s
GasSeparationTechnology
GasSeparationApplication
Hydrogen
Ammonia Refining
Chemical Synthesis
Nitrogen
EOR
Misc Apps
CO2
Gas Processing
EOR
Dehydration
Gas Processing
Air Separation
Absorption
Adsorption
Membranes
SmallerScaleApplications
LargestScaleApplications
Cryogenic
Distillation
H2S / CO2
Gas Sweetening CO2
Food/Chem Grade
O2 / N2
Merchant Production
O2 Enriched Air
Catalytic Cracking
Sulfur Recovery
Hydrogen
Steam Cracking

4. CCS Overview
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5. Definition of CO2 Capture
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Separation of the CO2 from a gas stream produced in a
power station or an industrial process to obtain pure
CO2 for geological sequestration or further use

6. Processes/Systems for CO2 Capture
SUPPORTED BY:
Capture routes
for power
generation
Classified by application

7. Solvent-Based Absorption
SUPPORTED BY:
• Chemical Absorption
Gas and solvent form chemical bonds
Faster kinetics than physical
Useful for low P operations (post-combustion)
Requires significant amount of energy to regenerate –
reversing chemical reaction
• Physical Absorption
Gas and solvent form weak physical bonds
Useful for higher P operations (pre-combustion)
Does not require heat to regenerate but lose CO2
pressure

8. Physical vs. Chemical Solvents
SUPPORTED BY:

9. Post-Combustion Solvent-Based Capture
SUPPORTED BY:
• Current state of the art
• Standard solvent is a 30-40%-wt aqueous Mono Ethanol Amine (MEA)
Flue Gas
LP Steam
Cooling Water
Electric Power
CO2
Condensate
~130 °C
saturated
>95 % pure
90% captured
~40 °C
PC 12-14% CO2
NGCC 3-5% CO2

10. Advantages and Challenges of Solvent-Based
Post-Combustion Capture
SUPPORTED BY:
Advantages
• 70+ years acid gas scrubbing experience
• Allows good heat integration and
management (useful for exothermic rxns)
• Selective capture from low partial pressure
CO2 streams
Challenges
• Dilute chemical solutions due to viscosity and
corrosion
• High regeneration energy (aqueous phase
sensible heating, stripping)
• DHrxn and kinetics tradeoff
23%
3%
3%
38%
0%
10%
20%
30%
40%
50%
60%
70%
%IncreaseinCOE
Energy Penalty
Fuel
Variable O&M
Fixed O&M
Capital

11. Boundary Dam Amine-Based Capture System
SUPPORTED BY:
• World’s first
commercial-scale
power plant with a fully
integrated carbon
capture system
• 110 MWe coal-fired
power production unit
• 90% Capture
• Captured CO2 is
compressed and
transported off-site for
use in enhanced oil
recovery (EOR)
operations at a nearby
oil field

12. Selected Developers of Large Post-Combustion
Systems
SUPPORTED BY:
Amine based
• Shell (Cansolv)
• Mitsubishi Heavy Industries (KM CDR)
• Aker Solutions
• Fluor (Econamine FG+)
• Alstom/DOW
• Doosan/HTC
• Linde/BASF
Non-amine based
• Alstom (Chilled Ammonia Process)
• Siemens (PostCAP)

13. Pre-Combustion Solvent-Based Capture
SUPPORTED BY:
• Systems for the separation of CO2 from H2 (before combustion)
• Applicable to Integrated Gasifier Combined Cycle (IGCC) plants (15-
60 %vol CO2)
• State of art: chemical absorption with physical and chemical
solvents (commercially available processes)
 chemical solvents: e.g. Methyl Diethanolamine (MDEA)
 physical solvent: Rectisol and Selexol
 mixtures of chemical and physical solvents are also possible
• Overall efficiency penalty* in IGCC plants is 9-11 %-points (20-25%
less power output)
* Including CO2 compression to 110 bar

14. CO2 Absorption Using Physical Solvents
SUPPORTED BY:
Example of application in IGCC
40 °C
48 bar 21 °C
1.7 bar

15. Selexol Capture Process
SUPPORTED BY:
ShiftedSyngas
LP Steam
Cooling Water
Electric Power
CO2
Condensate
~40 °C
~35 bar

16. Pre-Combustion Capture at an IGCC Plant
SUPPORTED BY:
3D rendering IGCC 2 x 290 MWe (Kemper County, US)
Source: Southern
Company

17. Sorbent-Based CO2 Capture
SUPPORTED BY:
• Adsorption
 Gas and solid form bonds on surface of porous material
 Chemical and physical adsorption
 Many types – zeolites, carbon-based, carbonates
• Can have varying process designs/reactors
 Fixed bed – cycles between adsorption and desorption,
need multiple units for continuous operation
 Fluidized bed – continuous operation, good heat
integration, requires a durable catalyst
 Moving bed – allows continuous operation but can become
complex, requiring adsorption and desorption reactors

18. Sorbent-Based CO2 Capture - Operations
SUPPORTED BY:
• Pressure swing adsorption (PSA)
 Used widely in the hydrogen production industry
 Utilizes high pressure feed gas, so potentially useful
for pre-combustion capture
• Vacuum swing adsorption (VSA)
 Sometimes considered a subset of PSA
 Operates at ambient temperature and pressure
 Selective separation based on characteristics of gas
species
 Releases captured gas by applying vacuum
 Used for oxygen, nitrogen, and hydrogen production
• Temperature swing adsorption (TSA)
 Useful at lower pressures and therefore post-
combustion capture

19. Example Fluidized Bed Process Configuration
SUPPORTED BY:

20. Advantages and Challenges of Sorbent Based
Capture
SUPPORTED BY:
Advantages
• Some experience with solid systems (TSA-
dehumidification, PSA-H2 sep.)
• Low regeneration energy (no stripping steam,
low heat capacity substrates)
• High equilibrium capacity/surface area
• Hybrid sorbents (Shift + Capture)
Challenges
• Heat management
• Durability (attrition, chemical stability)
• Maintaining high mass transfer
• Pressure drop/Solids transport
• Scale-up
• Case study showing a
fixed bed industrial
capture system coming
up later in presentation

21. Oxy-Combustion Systems
SUPPORTED BY:
• Combustion with pure oxygen rather than in order to produce a high
CO2 concentration flue gas ready for compression and transport
• Applicable to retrofits but,
1. Air in-leakage must be minimized,
2. Flue gas recirculation is required (to avoid high combustion T
and maintain designed heat and mass transport characteristics)
N2
Oxygen
Fuel
CO2 (+ H2O)
OXY
COMBUSTION
Air
Air
Separation
Unit (ASU)

22. Example Oxy-Combustion System Design
SUPPORTED BY:
NEW
NEW NEW
EXISTING

23. Oxy-Combustion System Characteristics
SUPPORTED BY:
• Require only additional electric power (ASU), no heat (steam)
• Do not use chemical solvents
• Overall efficiency penalty* in coal fired power plants:
PC plants 7-10%-points (20-25% less power output)
NGCC plants 11-13 %-points (25-30% less power output)
Main Developers:
• Air Liquide, Air Products, Praxair, Linde, Babcock&Wilcox,
Doosan, Foster-Wheeler, Alstom, Jupiter Oxygen
*including CO2 compression to 110 bar

24. Air Separation Unit (ASU)
SUPPORTED BY:
• State of the art ASU is cryogenic separation: ~180 kWhe/tO2
• Commercial ASU producers: Air Liquide, Air Products, Praxair, Linde
• Alternatives: Ion and Oxygen Transport Membranes (ITM/OTM) but
not yet mature for commercial applications
ITM module
Source: Air ProductsSource: Air Liquide

25. CO2 Capture in Industrial Processes
SUPPORTED BY:
Industrial
Sector
Process
(CO2 sources)
Estimated year of
maturity
Oil refining Fluid Catalytic Cracker (FCC)
Residues gasification
Hydrogen from Synthetic Gas Reforming (SGR) *
2020-30
2015-20
Currently mature
Hydrogen from fossil
fuels/biomass
Coal/Biomass Gasification
Steam Methane Reforming
Currently mature
Currently mature
Natural gas processing Gas sweetening * Currently mature
Liquid fuel Synthesis Fisher-Tropsch process * Currently mature
Bio-fuels synthesis Ethanol *
Bio-synthetic gas (digestion) *
Currently mature
Currently mature
Chemicals Ammonia * Currently mature
Iron & Steel Blast furnace
Direct Iron Reduction (DRI) *
2020-30
Currently mature
Cement Calcinator 2020-30
* Near pure CO2 streams are produced as part of the existing process

26. Case Study - Air Products H2 Production
SUPPORTED BY:
• Global atmospheric, process and specialty gases,
performance materials, equipment and services
provider
• Serving industrial, energy, technology and
healthcare markets worldwide
• Fortune 500 company
• Operations in over 40 countries
• ~19,000 employees worldwide
• World’s largest third party hydrogen supplier
• $10B+ company

27. Steam Methane Reforming with CO2 Capture
SUPPORTED BY:
• Port Arthur, TX
(Hydrogen plant at
Valero Refinery)
• 90% CO2 capture
(Vacuum Swing
Adsorption) from 2
steam-methane
reformers (SMRs)
yielding 1,000,000 tons
CO2 /year
• ≈28 MWe cogeneration unit to supply makeup steam to
SMRs and operate VSA and Compression Equipment
• CO2 to Denbury pipeline for EOR in West Hastings oil field

28. Integrated Cogeneration and Hydrogen Plants
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29. Simplified Block Flow Diagram
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30. Vacuum Swing Adsorption Process
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31. Completed Capture System and Cogen Unit
SUPPORTED BY:
• 1st Unit initiated operation Dec. 2012, 2nd unit March 2013
• CO2 transported 158km and injected into Hastings Field to be
used for EOR

32. Project Challenges
SUPPORTED BY:
• Technical Challenges
 Integration with existing hydrogen business
 Technology Scale-up
• Economic Challenges
 Managing incentives
 Schedule
 Capital
• Retrofit project within active operating facility
 Operating and Maintenance Costs

33. Post-Combustion: Innovative Technologies
SUPPORTED BY:
Technology Test Stage TRL
POST-COMBUSTION
Amine-based solvents Demo 7-9
Advanced amine-based solvents Pilot 5-7
Amino-Acid salt solvent Pilot 5-7
Aqueous Ammonia solvent Demo 7-9
Precipitating solvents Lab/Bench 2-5
Two-phase liquid solvents Lab/Bench 2-5
Catalysed enhanced absorption Lab/Bench 2-5
Ionic liquids Lab/Bench 2-5
Temperature or Pressure Swing Adsorption with solid sorbents (TSA/PSA) Pilot 5-7
Calcium Looping (CaL) Pilot 5-7
Membranes Pilot 5-7
Cryogenic CO2 separation Lab/Bench 2-5
Technology Readiness Level (TRL):
1-2 = concept; 2-5 = lab/bench scale; 5-7 = pilot; 7-9 = demonstrations
Source: Global CCS Institute – Status Report 2014 (Nov 2014)

34. Pre-Combustion: Innovative Technologies
SUPPORTED BY:
Technology Test Stage TRL
PRE-COMBUSTION
Physical and chemical solvents Demo* 7-9
Ionic liquids Lab/bench 2-5
Pressure Swing Absorption Based (PSAB) Lab/bench 2-5
Ammonium Carbonate-Ammonium Bicarbonate process (AC-ABC) Pilot 5-7
Temperature or Pressure Swing Adsorption with solid sorbents (TSA/PSA) Lab/bench 2-5
Sorption Enhanced Water Gas Shift (SEWGS) Lab/bench 2-5
Sorption Enhanced Steam-Methane reforming (SESMR) Pilot 5-7
WGSRs membranes Lab/bench 2-5
Membranes Pilot 5-7
Cryogenic CO2 separation Concept 1-2
Technology Readiness Level (TRL):
1-2 = concept; 2-5 = lab/bench scale; 5-7 = pilot; 7-9 = demonstrations
Source: Global CCS Institute – Status Report 2014 (Nov 2014)
* The technology is commercial but its use for CO2 capture in IGCC is under demonstration

35. Oxy-Combustion: Innovative Technologies
SUPPORTED BY:
Technology Test Stage TRL
OXY-COMBUSTION
Atmospheric oxy-combustion Demo 7-9
Ion Transport Membranes (ITM) Pilot 5-7
Oxygen Transport Membranes (OTM) Lab/Bench 2-5
Pressurized oxy-combustion Pilot 5-7
Chemical Looping Combustion (CLC) Pilot 5-7
Technology Readiness Level (TRL):
1-2 = concept; 2-5 = lab/bench scale; 5-7 = pilot; 7-9 = demonstrations
Source: Global CCS Institute – Status Report 2014 (Nov 2014)
Chemical
Looping
Combustion

36. Thank you!
Ron.Munson@globalccsinstitute.com
INTRODUCTION TO CAPTURE, USE AND GEOLOGICAL STORAGE OF CO2
January 22-23 2015
University of Sonora, Hermosillo
SUPPORTED BY: