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• Develop a novel, CO2
capture solvent with:
• 90% Carbon capture efficiency
• 25% Increase in capacity vs MEA
• Less than 35% increase in Cost of Energy Services
Program Objectives
Program Objective: Develop novel solvent and process for post-combustion capture of CO2 from coal-fired power plants with 90%Capture efficiency, and less than 35% increase in cost of electricity
capture
BENCH-SCALE PROCESS FOR LOW-COST CARBON
DIOXIDE (CO2) CAPTURE USING A PHASE-
CHANGING ABSORBENT
DE-FE0013687
GE Global Research
Tiffany Westendorf
2016 NETL CO2 Capture Technology Project Review MeetingAugust 10, 2016
© 2015 General Electric Company - All rights reserved
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• Extensive screening of multiple solvents
• Absorbs CO2 very rapidly in the 40-50oC range
• High CO2 loading (>17% weight gain, >95% of theoretical value)
• Carbamate readily decarboxylates at higher temps
• Carbamate is solid new process configuration
2
3
5
Si
Me
Me
O Si
Me
Me
NH
H2N OH
O
Si
Me
Me
O Si
Me
Me
NH2H2N
CO2
-CO2
1
Si
Me
Me
O Si
Me
Me
NH
H3N O
OSi
Me
Me
O Si
Me
Me
NH
NH
O
O
O
O
Si
Me
Me
O Si
Me
Me
NH3H3N
4
intermolecular
H shift
intramolecular
H shift
GAP-0
GAP-0 carbamate salt
Chemistry of GAP-0 reaction with CO2
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0%
2%
4%
6%
8%
10%
12%
14%
16%
18%
0 2 4 6 8
mas
s %
CO
2ab
sorb
ed
CO2 partial pressure (bar)
GAP-0/CO2 Reaction Isotherms
45 C
100 C
140 C
160 C
0.0020 0.0022 0.0024 0.0026 0.0028 0.0030 0.0032 0.0034-7
-6
-5
-4
-3
-2
-1
0
1
2
ln(P
(psia
))
1/T (K)
MEA (lit)
MEA (exp)
MEA (calc)
GAP-0 (exp)
GAP-0 (calc)
M'D'M' (exp)
M'D'M' (calc)
DAB-0 (exp)
DAB-0 (calc)
• Lower vapor pressure vs. MEA
• Higher heat of reaction vs. MEA
• Lower heat capacity vs. MEA
• >11% Dynamic CO2 capacity @ 6 bara
absorb
desorb
GAP-0 Properties
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1 Make the solid(Spray absorption)
2 Move the solid(Pressurized solids transport)
3 Regenerate the solvent(CO2 desorption and solvent recycle)
1
2
3
Phase-Changing CO2 Capture System
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Project Structure
Budget Period 1: Design and Build [2014]
Spray absorber, extruder, desorber
Preliminary Technical and Economic Assessment
Go/No-go: 90% CO2 Capture, <$50/tonne CO2
Budget Period 2: Unit Operations Testing [2015]
Optimize individual unit operations separately
Solvent manufacturability study and EH&S risk assessment
Update Technical and Economic Assessment
Go/No-go: 90% CO2 Capture, <$45/tonne CO2
Budget Period 3: Continuous System Operation [2016]
Integrate unit ops into continuous system, generate engineering data for scaleup
Final Technical and Economic Assessment
Goal: 90% CO2 Capture, <$40/tonne CO2
3-year, $3M Project$2.4M DOE share1/1/2014 – 12/31/2016
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Absorber• Heat
management
• GAP-0 b-isomer• Atomizer fouling• Presence of water,
heat stable salts
Extruder• Energy efficiency
• Dynamic seal stability
Desorber• Thermal stability• Corrosion
Project• Solvent availability, cost• Expertise resources
Risk Assessment
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Absorber experiments – dry flue gas
• Designed experiment:
– 2-16% CO2, 150-200slm
– 0.9 - 0.6 mol GAP-0:mol CO2
• 30-220mL/min GAP-0
Solids produced at all conditions
• Statistics support linear model
– Significant terms: GAP-0 : CO2 ratio, Gas flow
– For maximum conversion:
• lower gas flow (longer residence time)
• lower GAP-0 : CO2 ratio (more excess CO2)
79.3% 70.5%
88%
81.1%
73.9%
85.2%
92.8%
85.4%
71.3%
% CO2
Gas flow rate
GAP-0:CO280.2-81.9%
74.4%
60-97% GAP-0 conversion
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Absorber experiments – humid flue gas
Dry – powder clings to dry windows
5vol% – solids impact wet windows
Dry – “cake flour”
6.5vol% – wet droplets impact wet windows
6.5vol% - “hair gel”(videos MVI_0155,
MVI_0162)
Mass balance: 1-3wt% water in rich phase
Expect higher water content at lower feed % CO2
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CO2-rich Slurry is an opportunity…
0
10
20
30
40
50
60
70
80
90
100
0 5 10 15 20 25 30
% A
ctiv
e a
min
e r
eta
ine
d
Days of continuous exposure
Thermal Degradation - 55% carbamate loading
120C_55%C_ 0%W 140C_55%C_ 0%W
120C_55%C_ 10%W 140C_55%C_ 10%W
• Replace extruder with less costly rich transfer method
• More efficient RLHX with fluid than solids
• Water inhibits urea formation
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Phase-Changing CO2 Capture Process Pivot
• Slurry handling / pump selection and integration• Desorber heat transfer performance (2 1 stage)• Cost impact of slurry
PIVOT:Dry Slurry
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Slurry handling & absorber/pump integration
Viscosity measurement pump selection Pump integration w/ spray absorber
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Continuous spray absorber operation
GAP-0 spray
50% CO2 capture
Absorber outlet Tdp
Absorber inlet Tdp = 39+/- 0.5°C
• Pump integration enables continuous operation
• CO2 capture % comparable to dry FG
16% CO2
0.6 GAP-0 : CO2
2% CO2
1.0 GAP-0 : CO2
16% CO2
1.0 GAP-0 : CO2
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Desorber performance
• Batch desorber experiments consistent with equilibrium isotherms
• Stable desorber T during continuous operation with upgraded HX
Hot oil T ~140°C
Desorber T ~133°C
Continuous slurry feed
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Economic analysis – 550MW net
• Replacement of all unit ops with carbon steel – inhibitors• Spray absorber optimized for slurry production• Enhanced desorption at low temperature – steam stripper
$66.4
$49.8 $48.9 $48.1$46.3
$45.3
$42
$47
$52
$57
$62
$67
$72
MEA Case 6H HeatIntegration
CarbonSteel
SteamStripper
SprayAbsorber
Co
st o
f C
O2
($
/to
nn
e)
Values based on 2011 dollars
Slurry
5wt% H2O
Scaled
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Future Work
• Current Project
– Continuous System testing and optimization
– Develop scale-up strategy
– Prepare final TEA (target <$40/tonne CO2)
• Next Project: De-risk solvent management
– Advanced desorption/steam stripper
– Oxidative stability
• Scale-up Potential
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Thank You
• NETL• David Lang, Lynn Brickett, Elaine Everitt
• GE GRC Project Team• Mike Bowman, Stanlee Buddle, Joel Caraher, Wei Chen, Mark Doherty,
Rachel Farnum, Mark Giammattei, Terri Grocela-Rocha, Dan Hancu, Barbara Miebach, Robert Perry, Gosia Rubinsztajn, Surinder Singh, Irina Spiry, Paul Wilson, Benjamin Wood
17DE-FE0013687
3/4/2016
Acknowledgement . The information, data, or work presented herein was funded in part by the Advanced Research Projects Agency – Energy (ARPA-E), U.S. Department of Energy, under Award Number DE-AR0000084 and DOE- NETL under Award Number DE-NT0005310.
Disclaimer. The information, data, or work presented herein was funded in part by an agency of the United States Government. Neither the United States Government nor any agency thereof, nor any of their employees, makes any warranty, express or implied, or assumes any legal liability or responsibility for the accuracy, completeness, or usefulness of any information, apparatus, product, or process disclosed, or represents that its use would not infringe privately owned rights. Reference herein to any specific commercial product, process, or service by trade name, trademark, manufacturer, or otherwise does not necessarily constitute or imply its endorsement, recommendation, or favoring by the United States Government or any agency thereof. The views and opinions of authors expressed herein do not necessarily state or reflect those of the United States Government or any agency thereof.