pradeep indrakanti presentation
TRANSCRIPT
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Comparative Evaluation of
Post-Combustion CO2
Capture Technologies
Methodology to Evaluate The Performance of
CO2
Separation Technologies
- Solvents & Sorbents
-Pradeep Indrakanti
16/13/11
Acknowledgments
RECS, DOE-HQ and NETL LTI
Christopher Munson, Vince Brisini, John Huston,Scott (Shiaoguo) Chen, Rick Noceti
JMEnergy Consulting John Marano
Disclaimer
Reference in this presentation to any specific commercial product, process, or service by
trade name, trademark, manufacturer, or otherwise does not necessarily constitute orimply its endorsement, recommendation, or favoring by the United States
Government or any agency thereof. The views and opinions of author expressed in
this presentation are his own, do not necessarily state or reflect those of the United
States Government or any agency thereof.
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Outline
Introduction to cost/performance analysesChallengesCostsExamples of rigorous comparative analyses
Methodology to compare the performance ofsolvents, sorbents (not across categories)
Aqueous solventsSorbents
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Post-Combustion CO2
Capture
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Source: DOE/NETL Advanced carbon dioxide
capture R&D program: Technology update: May
2011
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
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Technical Challenges
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Adapted from DOE/NETLAdvanced carbon dioxide
capture R&D program:
Technology update: May
2011
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Costs
Levelized Cost of Electricty (LCOE) Capital Operations & Maintenance (O&M)
Fixed, Variable Fuel
f(energy efficiency or energy penalty of the overall plant) Transportation, Storage and Monitoring (TS&M)
Goal DOE cost goal: 35% LCOE increase over a (PC) plant
without CCS @ 90% capture (same net power)
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
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Advantages & Challenges
Solvents
Fast kinetics Good heat
integration
Experience High energy
(steam) load
Non-reactivecarrier fluid
heating
Sorbents
Fast kinetics, largecapacities
Lower heatrequirement
(solvents)
Heat requirement Heat transfer,
pressure drop
issues
Sorbent attrition6/13/11 7Source: DOE/NETL Advanced carbon dioxide capture R&D
program: Technology update: May 2011
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Membranes
No steam load No chemicals Flue gas
compression
% recovery vs.recovery rate
tradeoff
Multiple stages,recycle streams
Where is this type of
analysis relevant?
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PreliminaryAssessment
(solvent/processscreening or
evaluation)
PC plant simulation +Simple
CO2 capture models
Lab-, bench-scalestudies on new
solvents, sorbents,membranes
PC plant simulation +CFD CO2 capture
models (co-simulation)
Pilot plant/
Slipstream studies
Estimatesmay vary
as muchas 35%
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
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Example of a bottom-up cost analysis(Data from NETL/DOE post-combustion capture pathway study, preliminary
results, DOE/NETL Advanced carbon dioxide capture R&D program: Technologyupdate: May 2011)
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31.7
59.6 56.1 55 50.4 46.9 42.9
8
1312.3 12.2
11.210.6
9.85
8.78.3 8.6
7.67.1
8.414.2
19.618.8 18.4
16.715.1
15.4
5.65.2 5.2
54.8
4.8
20%
25%
30%
35%
40%
0
20
40
60
80
100
120
SCPC
SCPC
,FluorE
conamin
e
SCPC,Fluor
Econam
ine,enh
anced
SCPC,M
HIKS-1
USCPC,
MHIKS
-1
Advance
dmemb
rane,shockw
avecom
pression
Advance
dadsorber,sh
ockwave
compres
sion
Efficiency,
HHV
FirstyearCOE,
$/MWh
(mills/kWh)
Capital Fixed O&M Variable O&M Fuel
TS&M COE goal %HHV
TakeawayCapital cost
Fuel costFixed O&M
SCPC:
Supercritical
pulverized
coal powerplant
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Comparison of Various PC CCS
AnalysesIEAGHG Cost and Performance of CO2Capture from Power Generation, IEAWorking Paper, Finkenrath
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Note correlation between increased LCOE and efficiencydecrease
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Credits:The Far Side
Gallery 4
by Gary Larsen
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A Simplified Case for Aqueous
Solvents
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Sensibleheat
Heat of CO2desorption,
Latent heatof waterevaporation
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Flue gas fromdirect-contact
cooler
Flue gas, 90%CO2 removed
Absorptioncolumn
Strippercolumn
Reboiler
CO2 tocompression
Steam
CO2 + H2O
T
Lean-richheat
exchanger
Leansolution
Richsolution
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Econamine FG Plus flow
diagram
Source: Bituminous coal baseline,DOE/NETL-2010/1397
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Solvents: Energy Requirement
Qrxn : Heat required to drive CO2 out of solution (break solvent-CO2 bonds, heat of mixing, heat of solution) Hrxn
Qsensible : Heating the solvent without phase change Mass of solution/kg CO2*specific heat of solution*change in temperature
Cp*TLean-Rich HX/Cw , where Cw is the solution working capacity Cw = *xsolvent*MCO2/Msolution
Qwater_evap : Amount of water evaporated/kg CO2 * Latent heat ofvaporization
pH2O/(Pstripper ovhd- pH2O)*Hvap(H2O) [ Assumed pH
2O vapor pressure ]
Electrical equivalent of thermal energy (Weqregen)
6/13/11 140.75)*)/(M/PR.T.ln(P+.Q)T
T-0.75.(1=W
2COdesseq
th
regensteam
condeq
regen
Qthregen
INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Electrical Energy = Electrical energy equivalent of steam used forCO2 Capture + Compression Work
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Recap: Parameters Required
Solvent/solution properties Heat of reaction Hrxn, Specific heat capacity Cp, Solution working capacity Cw
(difference of rich and lean loadings, molecular weight of solution, mole fraction of solvent) Other
TLean-Rich HX, Stripper overhead pressure, temperature, Steam temperature, condenser water temperature
Caveat: Parameters are not independent of each other
Ex: Lower solvent working capacity (or higher lean loading)
lower heat exchangerT
Capex, opex increased L/G ratio
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
30 wt% aq. MEA (7m)
Rich solvent loading, mole CO2/mole MEA 0.484
Lean solvent loading, mole CO2/mole MEA 0.242
Net solvent loading, () mol CO2/mol MEA 0.242
Solvent Cp, kJ/(kg-K)* 3.7
Mole fraction of solvent in solution (Xsolvent)* 0.11
Molecular weight of solution (Msolution), kg/kg-mole* 22.83
Solvent working capacity, kg CO2/kg solventCw = *xsolvent*MCO2/Msolution
0.05 (0.242*0.11*44/22.83)
T (lean-rich HX), C 10
Hrxn, kJ/g-mol CO2 82
Tabsorber, C 40
Tstripper overhead, C 95
Tstripper bottom, C 120
Pstripper overhead, atm 1.8
Hvap, H2O, kJ/g-mol H2O 41
Solvents: Base Case
*: Used tocalculatesolvent
workingcapacity
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
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MEA Energy Penalty
Qthregen : 3237 kJ/kg CO2 NETL bituminous coal
baseline comparison:
3556 kJ/kg CO2
Breakdown (kJ/kg CO2) Qrxn : 1864 Qsensible : 707 Qstripping :666
Energy penalty: 24% < 30% because 130 C steam
(~3 bar)
210 C: ~31% energy penalty. Electrical equivalent of work
0.248 kWh/kg CO2 Reboiler steam at 130 C (266
F)
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
30 wt%MEA
30% MEA,Hi T(HX)
MEA Case1
MEA Case2
MEA Case3
(rich-lean gas molar loading), mole CO2/
mole solvent0.242 0.242 0.257 0.121 0.12
Cp solvent, kJ/kg/K 3.7
-Same as base case-Xsolvent, mole solvent/mole solution 0.11
Molecular weight of solution, kg/kg-mole 22.83
Solvent Working Capacity, Cw, kg CO2/kgsolvent
0.052 0.052 0.056 0.026 0.0268
T, lean-rich HX, K 10 20 10 5 5
Hrxn, kJ/mol CO2 82 -Same as base case-
CO2 absorpt ion T, C 40
-Same as base case-Tstripper, top, C 95
Tstripper, bottom (reboiler), C 120
Overhead pressure, atm 1.8 1.8 1.6 1.6 1.6
pH2O, overhead, atm 0.75 -Same as base case-
kg H2O/kg CO2
Hvap (H2O), kJ/kg H2O 41 41 41 41 41
Qrxn, kJ/kg CO2 1864 1864 1864 1864 1864
Qsensible, kJ/kg CO2 707 1415 666 707 690
Qwaterevap, kJ/kg CO2 666 666 823 823 823
Total heat consumption/stripping heat, QreboilerkJ/kg CO2
3237 3945 3353 3394 3377
Electricity equivalent of heat, WE, kJ/kg CO2 543 662 562 569 566
Compression Work, WC @75%, kJ/kg CO2 349 349 358 358 358
Total stripping+comp work, kWhe/kg CO2 0.2477 0.2807 0.2557 0.2576 0.2568
Auxiliary loads 3% 3% 3% 3% 3%
Total energy penalty 23.9% 26.7% 24.6% 24.8% 24.7%
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
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Adsorbent CO2 Capture
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Source: NETL In-House Postcombustion Sorbent-Based Carbon Dioxide Capture
Research, Pennline et al., Annual IEP Contractors Meeting, March 24, 2009
Moving Bed
CO2 adsorber
Fluegas
tostack
Flue gasto
adsorber CW
Rich
sorbent to
regenerati
on
(stripping)
Lean sorbentto adsorber
Steam In
CO2 to(compression/
recovery)
Sorbents:
Theoretical Regeneration Energy
0.75)*)/(M/PR.T.ln(P+.Q)TT-0.75.(1=W
2COdesseq
th
regensteam
condeq
regen
20
sorbent
CO2
water
}.TCp.TCp+H{O/wtCOwtH
+.TCp.TCp+H
+C)T-(TCp
=Q
adssorbdessteamdesO,H22
adssorbdesCOdes,CO
w
adsdessorb
regen
2
22
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Thermal Regeneration EnergyHeating sorbent, desorbing CO2, heating CO2,
desorbing & heating water
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Adsorbents: Base Case & ParameterVariations
Base Case Sorbent CO2 capacity: 1.7 g-mol
CO2/kg sorbent (7.5 wt%)
Enthalpy of CO2 desorption: 650BTU/lb CO2 (66.5 kJ/g-mol CO2)
CO2 adsorber temperature: 333K**
Desorption temperature: 378 K** Auxiliary Power: 3% of gross
power
Steam temperature: 388 K Enthalpy of water desorption: 40kJ/g-mol H2O Mass H2Odesorbed/Mass CO2 :
0.05
Parameters Varied
Enthalpy of CO2desorption: 650, 450
BTU/lb CO2 (66.5 to 46.1
kJ/g-mol CO2)
Sorbent CO2 capacity:1.7,3.0 g-mol CO2/kg
sorbent (7.5 to 13 wt%)
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**: Factors in Reactor Design for Carbon Dioxide Capture with Solid, Regenerable Sorbents, Hoffman et al. and field-scale testing (ADA).
: Lowest heat of adsorption measured for diamine-silica (SBA-15) : -48 kJ/mol
Cumulative Reduction in Energy PenaltyEffects of sorbent capacity and heat of CO2 adsorption
HH2O = 40 kJ/g-mole, mass H2O/CO2 = 0.05
46.1 kJ/molCO2, 13% Cw,
-2.68%
59.4 kJ/mol
CO2, 13% Cw,-1.66%
66.7 kJ/molCO2, 13% Cw,
-1.11%
59.4 kJ/molCO2, 7.5% Cw,
-0.55%
MEA @ 3.2 GJth/T
CO2, 10 K T
12%
14%
16%
18%
20%
22%
24%
Ene
rgyPenalty%
Base: 66.5 kJ/g-mol CO2, 7.5 wt% Cw, 20.16% penalty
Enthalpy of CO2desorption
CO2Carrying Capacity
46.1kJ/mol
CO2,
13%
Cw
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Discussion & Conclusions
Comparative Analyses LCOE = f( Capital Costs, O&M, Fuel Cost..) Fuel Cost = f(Energy Penalty, Type of Boiler..) Energy Penalty = CO2 Separation + Compression +
Auxiliary Work
Going forward Correlation between COE and energy penalty not
always positive What parameter combination results in lowest
COE?
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A
Questions
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INTRODUCTION EXAMPLES SOLVENTS SORBENTS Q&A