Electrochemically-mediated Sorbent Regeneration in CO ... · Mike Stern Aly Eltayeb. Ryan Shaw....
Transcript of Electrochemically-mediated Sorbent Regeneration in CO ... · Mike Stern Aly Eltayeb. Ryan Shaw....
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Electrochemically-mediated Sorbent Regeneration in CO2Scrubbing Processes
NETL Pittsburgh, PA | August 26, 2019
Principal Investigator
Professor T. Alan [email protected]
Submitted toU.S. Department of Energy
Office of Fossil EnergyNational Energy Technology Laboratory
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Project Overview
Award Name: Electrochemically-Mediated Sorbent Regeneration in CO2 Scrubbing Processes (FE0026489)
Funding: DOE $1,202,052 Cost Share $ 310,601 Total $1,512,653
Project Period:August 1, 2017 – December 31, 2020
Project PIs: T. Alan Hatton, Howard HerzogDOE Project Manager: Ted McMahon, Bruce Lani, David Lang
Overall Project Objectives: Develop, characterize and implement electrochemically mediated sorbent regeneration and CO2 release in amine scrubbing processes
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Amine Regeneration in CO2 Capture
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Electrochemically Mediated Amine Regeneration
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Electrochemically Mediated Amine Regeneration
5T < 60°C
T = 40-80°CP = 1 -10 barE ~ 0.5 V/cell
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Nernstian Description of Electrochemical Gas Separation Cycle
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2
2
ln anode
cathode
Cucell
Cu
aRTEnF a
+
+
=
( )2 21 17, ,..., , ,o
CO in AmCuE f a K K y C+=
2
:2 o
Cucopper loadingAm
+
=
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Nernstian Description of Electrochemical Gas Separation Cycle
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2
2
ln anode
cathode
Cucell
Cu
aRTEnF a
+
+
=
( )2 21 17, ,..., , ,o
CO in AmCuE f a K K y C+=
C
A
2
:2 o
Cucopper loadingAm
+
=
B
D
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Prior effort: EMAR CO2 capture
0.0
2.0
4.0
6.0
8.0
10.0
0 0.1 0.2 0.3 0.4 0.5 0.6
CO
2 Ab
sorb
ed (m
L/m
in)
Current (A)
Theoretical Max
Experiment
0.0
0.1
0.2
0.3
0.4
0.5
0.6
0 0.2 0.4 0.6 0.8 1
CO
2 Loa
ding
, Φ
Copper Loading, η
EDA
TETA
AEEA
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EMAR Advantages and Challenges
Advantages:• Does not need steam and extensive retrofitting• Lower operation temperature• Can desorb at pressure• Can utilize low grade waste heat to improve
efficiency
Challenges:• Overpotentials intrinsic to electrochemical
systems• Efficiency losses due to ion migration• Stable cyclic operation
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Technical Approach
Evaluation of amine-metal pairs Thermodynamics Kinetics
Electrochemical characterization Evaluate supporting electrolyte Overpotentials required
Electrochemical cell modelingProcess modeling
Energetics Techno-economic analysis
Bench scale demonstration
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RDE results imply asymmetrical electrode polarization
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• Chronoamperometry on rotating disk electrode shows overpotential (η) for cathodic reaction
• Higher overpotential with increasing CO2 content
2 2
2( ) ~ ~ 0.3( )
o
o
o
CO CO
PK
i EDA CP
Oi EDA
α
−
2 (2 )
1/2 3/
2
4
(1 )2 [ ] [ ( )
~ 1 )
]
2(o o
oi
i Fk EDA Cu EDAα α
η η
+ −
−
=
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Supporting salt affects kinetics
• Changing electrolyte can increase current density from <10 mA/cm2 to >50mA/cm2
• Addition of Cl- increases current density to 100 mA/cm2
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EMAR Cell Construction
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Continuous Bench Scale EMAR
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Gas Separation and Electron Utilization: Effect of Flow Rate
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Voltage and Gas Evolution with Varying Current
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Continuous Operation under Constant Current
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Enhanced Electrode Stability with Recycle
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40 hr with no recycle 200 hr with recycle
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EMAR thermodynamics modeling
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Wolery, (2002); Paoletti, Pure Appl Chem, 56, (1984): 491-522; Stern, PhD Thesis, (2013)
EMAR electrolyte speciation with copper electrodes and EDA as the amine
To calculate:• Electrochemical Energetics• Process energetics (compressor, pump, hot water utilities, etc.)
Hatton Group, Int. J. Greenhouse Gas Control. 2019, 82, 48-58.
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Thermodynamics modeling validation
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CO2 capacity/loading measurements at 50°C under different fCO2 and cCu
Hatton Group, Int. J. Greenhouse Gas Control. 2019, 82, 48-58.
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Electrochemical Energetics
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T = 50°C, 1m EDA + 0.5m Na2SO4 + 0.25m CuSO4
to : Oxidation
Cu(s) Cu2+ + 2e−1 2 to : Reduction
Cu2+ + 2e− Cu(s)
2 3
min
𝑊𝑊min =1
𝐹𝐹m,CO2�𝑥𝑥Cu
𝐸𝐸oxd𝐼𝐼 − �𝑥𝑥Cu
𝐸𝐸redd𝐼𝐼 𝑊𝑊min,corrected =1
𝐹𝐹m,CO2�𝑥𝑥Cu
𝐸𝐸oxd𝐼𝐼 − �𝑥𝑥Cu
𝐸𝐸redd𝐼𝐼 𝑊𝑊EMAR =1
𝐹𝐹m,CO2�𝑥𝑥Cu
𝐸𝐸oxd𝐼𝐼 − �𝑥𝑥Cu
𝐸𝐸redd𝐼𝐼
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Minimum EMAR Work: Co-Current Operation
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anode
cathode
T = 50°C, 1m EDA + 0.5m Na2SO4 + 0.25m CuSO4Ionic current via SO4
2- migration
1
1
2
2
3 4
3
4
1
23
4
0 1x
NOT A LINEAR SCALE !
∆V
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Finite Electrode Overpotential: Segmented Electrodes
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T = 50°C, 1m EDA + 0.5m Na2SO4 + 0.25m CuSO4Ionic current via SO4
2- migration
cath
ode
anod
e
2
1 3
4
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EMAR Work with Segmented Electrodes
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cath
ode
anod
e
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Effect of Operating Parameters on Overall Energetics
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Base case
Tabs = 50°C, Tdes = 50°CCu Shift = 60% Pdes = 1 bar, overpotential = 0.1V
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Process Energetics comparison
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55°C55°C
155°C
129°C~125°C
1 2 3
[1] Econamine process, Case10, Rev.2a, NETL (2013) [2] Rabensteiner et al., Int J Greenh Gas Con, 27 (2014), 1-14 [3] Lin and Rochelle, Chem Eng J, 283, (2016): 1033-1043
/Steam utility
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Cost of Electricity and CO2 Avoided
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Purchased equipment component cost
breakdown
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Effective and stable approach for flue gas CO2 capture
Favorable energetics and costs relative to conventional thermal amine processes
A high electron utilizationof 0.8mol CO2 per mol e
EMAR is an alternative CO2 desorption at low temperature (less amine degradation) and with electricity (easier retrofit)
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Conclusion
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Project Risks and Mitigation Strategies
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Technical Risks Probability Impact Risk MitigationCO2 sorbents and metal ion systems unsuccessful
Medium Low Wide range of candidate sorbents available. Initial results are promising
Electrochemical cell models low in fidelity and do not permit optimization
Moderate Low Complexity of underlying mechanisms in electrochemical cell presents risk for modeling. Parametric experiments will generate sufficient data for empirical optimization.
Process found to be too sensitivefor long-term operations and disturbances
Moderate Moderate Preliminary testing is encouraging. Degradation of electrodes or sorbents possible, but can be mitigated through design of electrode configurations
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Resource and Management Risks
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Resource Risks Probability Impact Risk MitigationCost of bench-scale system after optimization more expensive than planned
Low Low Most of the components of the system have been procured and operated in previous work, but the optimized system might involve more expensive equipment, especially for automation.
Management Risks Probability Impact Risk MitigationProcess performance reaches a plateau that does not satisfy DOE research goals
Moderate High The progress reports will allow the project team to evaluate the performance of the process and determine whether it is possible to explore new dimensions for performance improvements.
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Acknowledgement
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Mike Stern Aly Eltayeb Miao WangRyan Shaw Subrahmaniam Hariharan