y. riachi, d.clodic 9 th annual ccs conference pittsburgh pennsylvania may 10-13 2010 ctsc chaire...

Y. Riachi, D.Clodic

9th Annual CCS Conference Pittsburgh Pennsylvania

May 10-13 2010

CTSC Chaire

Paris, 01/12/2010

Chair CO2 – 01/12/2010 - P 2

Agenda

Post combustion.

Chemical Looping.

Oxy-combustion.

Chair CO2 – 01/12/2010 - P 3

Post combustion

Latest Advancements in Post Combustion CO2 Capture Technology for Coal Fired Power Plant

Steve Holton Mitsubishi Heavy Industry

Chair CO2 – 01/12/2010 - P 4

Post combustionMitsubishi Heavy Industry

KS-1TM solventSteam consumption:

*1.30 Ton Steam/Ton CO2

*660 kcal/kg CO2 Recovered

Note: Steam 3 Bars G. Saturated

Natural Gas flue gas CO2 Recovery

Chair CO2 – 01/12/2010 - P 5


KS-1TM solventIncreased CO2 loadingSteam consumption:

*1.2 Ton Steam/Ton CO2

*620 kcal/kg CO2 Recovered

Note: Steam 3 Bars G. Saturated

Reduced, by 30% over MHI’s Conventional ProcessFurther improvements 0.85 - 1 Ton Steam/Ton CO2

Natural Gas flue gas CO2 Recovery

Chair CO2 – 01/12/2010 - P 6


Impurities in the Coal Fired Flue Gas depend on coal type and flue gas treatment conditions and should be clarified.

The following impurities have to be carefully treated before CO2 capture: SO2, SO3 ,NO2 Dust & particulates ,Hydro carbons

Accumulation and effects of coal flue gas impurities for CO2 Capture Plant have to be confirmed through long-term demonstration operation.

Coal fired flue gas CO2 Recovery

~6,000 hrs were achieved at a commercial coal-fired power station in Southern Japan on a 10 ton/d for CO2 Capture pilot

The MHI CO2 Recovery process can be applied to the flue gas of coal-fired boilers

Chair CO2 – 01/12/2010 - P 7

Post combustion

Evaluation of a Hot Carbonate Absorption Process with High Pressure Stripping

Enabled by Crystallization

Shiaoguo Chen Carbon Capture Scientific LLC

Chair CO2 – 01/12/2010 - P 8

Post combustionHot Carbonate Absorption Process with High-Pressure Stripping Enabled by Crystallization

HOT – CAP process flow diagram

Chair CO2 – 01/12/2010 - P 9

Post combustionHot Carbonate Absorption Process with High-Pressure Stripping Enabled by Crystallization

Coal-fired flue gas CO2 Recovery

Chair CO2 – 01/12/2010 - P 10

Post combustionHot Carbonate Absorption Process with High Pressure Stripping Enabled by Crystallization

High-stripping pressure low compression work low stripping heat (high CO2/H2O partial pressure ratio) Low sensible heat Comparable working capacity than MEA Low Cp (~1/2) Low heat of absorption 7-17 kcal/mol CO2(heat of crystallization incld.) vs. 21

kcal/mol for MEA Kinetics improved by employing high-concentration PC and

high-absorption temperature FGD may be eliminated No solvent degradation Low-cost solvent Less corrosiveness

Chair CO2 – 01/12/2010 - P 11

Post combustion

Concentrated Piperazine A Case Study of Advanced Amine Scrubbing

Gary T. Rochelle The University of Texas at Austin

Chair CO2 – 01/12/2010 - P 12

Post combustionConcentrated Piperazine A Case Study of Advanced Amine Scrubbing

Process flow diagram

Wideal = 113 kwh/tonne, Wreal = 219 kwh/tonne

Chair CO2 – 01/12/2010 - P 13

Post combustionConcentrated Piperazine A Case Study of Advanced Amine Scrubbing

Conclusions

A published amine that requires only 2.6 MJt or 220 kwhe /tonne CO2

10-20% less energy than 30 wt% MEA Double the CO2 mass transfer rate 1.8 x capacity Stripping at 150°C and 11-17 atm

Superior Solvent management Thermally Stable Oxidatively stable Less volatile than 7 m MEA Good Opportunities for Reclaiming

Chair CO2 – 01/12/2010 - P 14

Post combustion

Post-Combustion CO2 Capture TechnologyPilot Performance and

Scale-Up Analysis

Phillip Boyle Powerspan Corp

Chair CO2 – 01/12/2010 - P 15

Post combustionPost-Combustion CO2 Capture Technology Pilot Performance and Scale-Up Analysis

2008 Powerspan Corp. has been testing its post-combustion

ECO2® carbon capture technology. 1-MWe pilot facility located at First Energy's R.E. Burger Plant near

Shadyside, Ohio. 2009 Enhancements to the pilot configuration and solvent chemistry Improved performance. 2010 Assessment of the design, operation, and performance of the

ECO2 pilot, Implications of test results from the ECO2 pilot for new and

retrofitted coal-fired power plants (200 MW and larger units)

Chair CO2 – 01/12/2010 - P 16


The steam extraction demand

is 388,840 lbs/hr.

Demands

Chair CO2 – 01/12/2010 - P 17


Subcritical The net output of the plant is reduced by about 30%, The plant net efficiency is reduced by 9.97%. Supercritical The contribution of the LP turbine section to total power

generation in a subcritical steam cycle is relatively high compared to the corresponding contribution in a supercritical steam cycle.

The extraction of LP steam prior to the LP turbine results in a higher percentage of power loss for a subcritical unit than would be the case for a supercritical unit.

The higher CO2 production per MWh for the subcritical case requires more steam for regeneration and more electrical power for compression than would occur for a more efficient plant.

Impact on power plant efficiency

Chair CO2 – 01/12/2010 - P 18


Cost estimate and economic analysis

Chair CO2 – 01/12/2010 - P 19

Post combustion

Chilled Ammonia Field Pilot Program at We Energies

Fred Kozak Alstom

Chair CO2 – 01/12/2010 - P 20

Post combustionChilled Ammonia Field Pilot Program at We Energies

Simplified Process Schematic of the Chilled Ammonia Process (CAP) at We Energies

2NH3 + H2O + CO2 = (NH4)2CO3 (1) NH3 + H2O + CO2 = (NH4)HCO3 (2) H2O + CO2 + (NH4)2CO3 = 2(NH4)HCO3 (3) (NH4)2CO3 + NH3 = NH2COONH4

(4) SO2 + 2NH3 + H2O ⇒ (NH4)2 SO3 (5) (NH4)2SO3 + 1/2O2 ⇒ (NH4)2SO4 (6)

Chair CO2 – 01/12/2010 - P 21


Total Operating Hours Through Oct 2009 – 7717 The CO2 capture efficiency ranged from 80 to 95%, with an

average of 88.6% across the entire period CO2 purity is consistently above 99% with a moisture

content in the range of 2,000 to 4,000 ppmv and an ammonia content of less than 10 ppmv.

CO2 capture efficiency and purity

Chair CO2 – 01/12/2010 - P 22


The average of five data points showed the CAP power requirement to be 200 kWh/ton of CO2 delivered at 300 psig (21 bar(g)).

Energy utilization

1210 kJ/kg

Chair CO2 – 01/12/2010 - P 23

Post combustion

Effects of Coal Type andTurbine Cycle Characteristics

on Post-Combustion CO2 Capture

Edward LevyLehigh University

Chair CO2 – 01/12/2010 - P 24

Post combustionEffects of Coal Type and Turbine Cycle Characteristics on Post-Combustion CO2 Capture

Effect of Coal type and steam cycle on unit performances Steam cycle

Subcritical cycle Supercritical cycle Coal type Bituminous PRB

Chair CO2 – 01/12/2010 - P 25


LT turbine power loss

CO2 compressor power consumption

Chair CO2 – 01/12/2010 - P 26


LT turbine power loss

Optimized extraction point

Lower steam pressure and temperature at the steam extraction point, reduces the turbine power loss

Reducing stripper pressure level increases the heat needed for solvent regeneration and CO2 compressor power

An optimal extracting steam pressure from the LP turbine to operate the stripper reboiler minimizes the unit net power loss

Chair CO2 – 01/12/2010 - P 27

Post combustion

A new high-performance scrubbing agent for the separation of CO2 from various gas streams

Matthias Seiler EVONIK Degussa

Chair CO2 – 01/12/2010 - P 28

Post combustionA new high-performance scrubbing agent for the separation of CO2 from various gas streams

1. Presentation of a new high-performance CO2 -absorbent made by Evonik Degussa

2. Performance characterization 3. Comparison with other state-of-the-art CO2 absorbents

Chair CO2 – 01/12/2010 - P 29

Post combustionA new high-performance scrubbing agent for the separation of CO2 from various gas streams

Absorption capacity of Evonik absorbent 1.7 times betterthan MEA

Cyclic capacity of Evonik absorbent 1.7 –2.4 times betterthan MEA

Corrosion for Evonik absorbent Factor 10 better/ lower than for MEA

Absorption kinetics of Evonik absorbent as good as MEA Absorption enthalpy of Evonik absorbent 50% better/ lower

than MEA Viscosity of Evonik absorbent comparable to MEA Chemical stability of Evonik absorbent appropriate Volatility of Evonik absorbent better/ lower than MEA

Chair CO2 – 01/12/2010 - P 30

Chemical looping

Water Vapor Impact on Oxygen Carrier

Performance for Chemical Looping Combustion of Solid Fuels

University of Kentucky,

Center for Applied Energy Research

Chair CO2 – 01/12/2010 - P 31

Chemical loopingWater Vapor Impact on Oxygen Carrier Performance for Chemical Looping Combustion of Solid Fuels

Water vapor improves the rate and completeness of direct char combustion with OCs by facilitating in-situ gasification.

The influence of OC particle size on direct char combustion process was also examined by thermogravimetric analysis. The results show no significant difference among the five size ranges.

Chair CO2 – 01/12/2010 - P 32

Chemical loopingWater Vapor Impact on Oxygen Carrier Performance for Chemical Looping Combustion of Solid Fuels

The results obtained from OC reductions in simulated syngas with and without adding 10% water vapor at 950°C show that the presence of water vapor causes reduction of OC performance in terms of oxygen carrying capacity and reactivity due to the formation of Fe3O4, an intermediate reduction product of Fe2O3.

TG examinations on pure Fe2O3 indicate Fe3O4 prevents the OC from further reduction to FeO. XRD analyses confirm the formation of Fe3O4.

Compared to the pure Fe2O3 powders, some of the freeze-granulated OCs show better resistance towards the water vapor effect possibly because the porous alumina supports provide better access of reactive gases to Fe2O3.

Chair CO2 – 01/12/2010 - P 33

Oxy-Combustion

Oxy-Combustion Technology Development

– Ready for Large Scale Demonstration

Carl Edberg Alstom power system

Chair CO2 – 01/12/2010 - P 34

Oxy-CombustionOxy-Combustion Technology Development– Ready for Large Scale Demonstration

The combustion of the fuel in a mixture of recirculated flue gas and almost pure oxygen results in changes in the combustion behavior as well as in the combustion products, which have some effects on the design of a boiler.

Simplified scheme of the Oxy-Combustion principle

Chair CO2 – 01/12/2010 - P 35


The main focus investigations for the oxy-combustion boiler

Chair CO2 – 01/12/2010 - P 36


Results

Chair CO2 – 01/12/2010 - P 37


Typical periods of time for standard procedures: Venting of boiler and flue gas paths: approx. 20 minutes Start of fire up to full load: approx. 45 minutes Switch from air to oxy-combustion mode: approx. 20 - 30

Dynamic process

Chair CO2 – 01/12/2010 - P 38


The post-combustion and oxy-combustion technology will be available commercially in 2015 for large scale plants (e.g. 800 MWe).

Results from the Vattenfall’s 30 MWth oxy-combustion pilot in Schwarze Pumpe (Germany) and the Alstom’s 15 MWth oxy-combustion pilot (BSF) in Windsor (USA) are very encouraging and support the commercial viability of the oxy-combustion technologies.

With a feasibility study executed by Vattenfall and recently completed with the involvement of Alstom, a decisive step towards industrial implementation of CO2 capture technology has been taken.

Jänschwalde (Germany) is a priority site chosen by the Vattenfall Group for large-scale demonstration.

Conclusions

Merci pour votre attention

y. riachi, d.clodic 9 th annual ccs conference pittsburgh pennsylvania may 10-13 2010 ctsc chaire...

Documents

chair co2

post combustion evaluation

agenda post combustion

recovery slide

flue gas of coal

kwhtonne slide

austin slide

corrosiveness slide