Chemical Looping Technology –Reaction, Reactor and Solids Flow

Issues

L. S. FanDepartment of Chemical and Biomolecular

Engineering The Ohio State University

Columbus, Ohio 43210

by

August 17, 2011

0

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0 20 40 60 80 100

% Electricity

Ov

era

ll P

roc

ess

Eff

icie

nc

y

0

10

20

30

40

50

60

70

80

90

SCL

Gasfication-WGS

IGCC-SELEXOL

Subcritical MEA

Ultra-supercritical MEA

Ultra-Supercritical Chilled Ammonia

Syngas CLC

H2 Membrane WGS

CO2 Membrane WGS

CDCL

Comparison Among Gaseous Chemical Looping, Direct Coal Chemical Looping and Traditional Coal to Hydrogen/Electricity Processes

Assumptions used are similar to those adopted by the USDOE baseline studies.

BasePlant

MEAPlant

CDCLPlant

Coal Feed, kg/h (lb/h)198,391

(437,378)278,956

(614,994)210,118

(463,231)

CO2 Emissions, kg/MWhnet (lb/MWhnet)856

(1,888)121

(266)~0

(~0)

CO2 Capture Efficiency, % 0 90 ~100

Solid Waste,a kg/MWhnet (lb/MWhnet)35

(77)49

(108)39

(87)

Net Power Output, MWe 550 550 550

Net Plant HHV Heat Rate, kJ/kWh (Btu/kWh)

9,788(9,277)

13,764(13,046)

10,357(9,817)

Net Plant HHV Efficiency, % 36.8 26.2 34.8

Energy Penalty,b % - 29 5

Aspen Plus® Modeling Results

aExcludes gypsum from wet FGD. bRelative to Base Plant; includes energy for CO2 compression.

Topics

• Two Types of Chemical Looping Systems

• Particle Synthesis and Ionic Diffusion Mechanism

• Modes of Reactor Operation

• Stability of Solids Flow

• Chemical Looping System Efficiency

• Commercialization Potential

5

Chemical Looping for Fossil Fuel Conversions

Two typical types of looping reaction systems

Oxygen Carrier (Type I)

Me/MeO, MeS/MeSO4

CO2 Carrier (Type II)

MeO/MeCO3

“1st Meeting of High Temperature Solids Looping Cycle

Network”, Oviedo, Spain, September 15-17 (2009).

“1st International Conference on Chemical

Looping”, Lyon, France, March 17-19 (2010).

Macroscopic Properties of Calcium OxideSintered_CaO

Hydrated_CaO

- Hydrated_CaO has smaller particles size - Hydration caused cracks on the surface

7

Fuels &

ChemicalsAir

Separation

Hydrogen

Fuel

Cell

Steam

Slag Steam

Turbine

Gas Turbine

Air

Compressor

Stack

HRSG

Rotary

Calciner

INTEGRATED

WGS +H2S

+COS + HCL

CAPTURE

Generator

Gasifier

BFW

To Steam

Turbine

CO2

Air

Air

Oxygen

CaO

CaCO3

Steam

H2+O

2

OSU Calcium Looping

Process

HeatOutput Heat

Input

Pure CO 2 gas

Calcination: CaCO 3 CaO + CO 2

CO + H 2O CO 2 + H 2

CaO + CO 2 CaCO 3

CaO + H 2S CaS + H 2OCaO + COS CaS + CO 2

Chloride CaO + HCl CaCl 2 + H 2O

Syngas

Hydrogen

reactor

RegenerationReaction

HeatOutput Heat

Input

Pure CO 2 gas

Calcination: CaCO 3 CaO + CO 2

WGSR : CO + H 2O CO 2 + H 2

CO2 removal : CaO + CO 2 CaCO 3

Sulfur : CaO 2S CaS OCaO CaS + CO 2

: CaO + HCl CaCl 2 + H 2O

Syngas

Hydrogen

Hydrogen reactor

CaCO3

CaO

Calciner

Calcium Looping Sub-pilot Unit for Hydrogen production

Air

Separation

Unit

Gasifier

Quench

Shift

Reactors

Syngas

Scrubber

2-Stage

Selexol

Coal Prep

and Feed

Slag

Handling

CO2

Compression

Dehydration

Pressure

Swing

Adsorber

Boiler

Radiant

Cooler

Syngas

Cooling

Mercury

Removal

Claus

Plant

Steam

TurbineCoal

Water

Air

Slag

Sulfur

Flue Gas

Pure H2

CO2

Air

220,904 kg/h

1316°C

56 bar

464,968 kg/h

677°C

56 bar

153 bar

0.999 v/v H2

≥ 22 bar

Base Coal-to-Hydrogen Process

Air

Separation

Unit

Gasifier

Coal Prep

and Feed

Slag

Handling

CO2

Compression

Dehydration

Pressure

Swing

Adsorber

Radiant

Cooler

Steam

TurbineCoal

Water

Slag

Pure H2

CO2

Air

220,904 kg/h

1316°C

56 bar

153 bar

0.999 v/v H2

≥ 22 bar

464,968 kg/h

677°C

56 bar Calcium

Looping

Process

Coal

Limestone

Solid Waste

CLP Coal-to-Hydrogen Process

CLP Process Flow DiagramCoal-to-Hydrogen Plant

Syngas

from

Radiant

Cooler

Coal

Solids Purge

Limestone

Expander Ca

rbo

na

tor

CycloneFiretube

Boiler

Condensing

Heat

Exchanger

Condenser

H2 to

PSA

PSA

TailgasCa

lcin

erVent Gas

AirASU

Hy

dra

tor

H2O

CO2 to

Compression

CO2 Recycle

Cyclone

Fabric

Filter

Condenser

CaCO3

CaO

Ca(OH)2

O2

HRSG

Lockhopper

Lockhopper

Ash

Indicates heat is

recovered for steam cycle

650°C

23 bar

Ca/C = 1.3 mol/mol

875°C

1 bar

677°C

56 bar

464,968 kg/hLockhopper

Cyclone

Exhaust

Gas

Coal-to-Hydrogen Case SMR Case

BasePlant

CLPPlant

BasePlant

CLPPlant

First-Year Capital ($/kg) $2.26 $2.58 $0.62 $0.96

Fixed O&M ($/kg) $0.43 $0.57 $0.16 $0.26

Fuel ($/kg) $0.36 $0.55 $1.22 $1.40

Electric Powera ($/kg) -$0.03 -$1.13 $0.14 -$0.70

CO2 Emissions ($/kg) $0.06 $0.00 $0.03 $0.00

Other Variable O&M ($/kg) $0.04 $0.14 $0.02 $0.05

TOTAL FIRST-YEAR COH ($/kg) $3.12 $2.72 $2.19 $1.98

TOTAL FIRST-YEAR COE ($/MWh) $105.00 $91.61 $105.00 $94.91

∆ = -13%

Economic Analysis ResultsCoal-to-Hydrogen and SMR Cases

aComputed using electricity price equal to the total COE value shown in the table.

∆ = -10%

13

ε ≈ 1

Partial oxidation

/Gasification

ε = 0.88

H2 + CO

407.7 kJ

358.9 kJ

0 Heat Loss

48.8 kJ Exergy Loss

Water Gas Shift

H2 +CO2

393.4 kJ

322.9 kJ

ε = 0.82

ε = 0.89

Fe

514.8 kJ

456.4 kJFe3O4 @1023K

(0.395 mol)

107.1 kJ

71.9 kJ

ε = 0.669

14.3 kJ Heat Loss

36 kJ Exergy Loss

H2 + Fe3O4

485.5 + 107.1 kJ

396.9 +71.9 kJ

ε = 0.82

Carbon

407.7 kJ/mol

407.7 kJ/mol

23.2 kJ Exergy Loss77.8 kJ thermal

energy @ 380 K

12.41kJ Exergy

ε = 0.16

Partial oxidation

I

II

Substance

Enthalpy of degradation

Exergy

Exergy Rate (ε)

Energy/Exery Loss

Additional Energy Input

Final Product

ε ≈ 1

Partial oxidation

/Gasification

ε = 0.88

H2 + CO

407.7 kJ

358.9 kJ

0 Heat Loss

48.8 kJ Exergy Loss

Water Gas Shift

H2 +CO2

393.4 kJ

322.9 kJ

ε = 0.82

ε = 0.89

Fe

514.8 kJ

456.4 kJFe3O4 @1023K

(0.395 mol)

107.1 kJ

71.9 kJ

ε = 0.669

14.3 kJ Heat Loss

36 kJ Exergy Loss

H2 + Fe3O4

485.5 + 107.1 kJ

396.9 +71.9 kJ

ε = 0.82

Carbon

407.7 kJ/mol

407.7 kJ/mol

23.2 kJ Exergy Loss77.8 kJ thermal

energy @ 380 K

12.41kJ Exergy

ε = 0.16

Partial oxidation

I

II

Substance

Enthalpy of degradation

Exergy

Exergy Rate (ε)

Energy/Exery Loss

Additional Energy Input

Final Product

I. Contional Process

Exergetic Efficiency

322.9/407.7 = 79.2%

II. Chemcial Looping Process

Exergetic Efficiency

396.9/(407.7 + 12.41)=94.5%

Exergy Analysis on Hydrogen Production

14

Historical Development of Chemical Looping Technologiesfor Fossil Energy Conversions

TechnologiesLane Process and

Messerschmitt Process

Lewis and

Gilliland ProcessIGT HYGAS Process

CO2 Acceptor

Process

Time Early Twentieth Century 1950s 1970s 1970s

Looping Media Fe/FeO/Fe3O4 Cu2O/CuO FeO/Fe3O4 CaO/CaCO3

Reactor Design Fixed bed Fluidized bed Staged fluidized bed Fluidized bed

Lane Process

Lewis and Gilliland Process

IGT Process

CO2 Acceptor Process

15

IGT Steam Iron HYGAS Process

MO=> M M=> MO

Gas Conversion (%) 65 45

Solid inlet 80% Fe3O4- 20% FeO 95% FeO- 5% Fe

Temperature (oC) 900 900

Reactor Fluid Bed Fluid Bed

– Poor solid phase conversions: Used only about 25% oxygen

capacity of the particles.

– Low gas phase conversions:

– Used iron ore: Low reaction rates

– Only about 40% efficient

– The process not geared towards making pure CO2

Poor Thermo

Recyclability of Commercial Fe2O3

17

Performance of Composite Fe2O3

0

50

100

150

200

250

300

350

400

450

Fresh

10 Cycles

100 Cycles

Forc

e (N

)

100 Cycle Pellet Reactivity

100 Cycle Pellet Strength

Oxygen Carrier Selection

Primary Metal Fe Ni Cu Mn Co

Potential Supports Al2O3, TiO2, MgO, Bentonite, SiO2, etc

Cost + – – ~ –

Oxygen Capacity1(wt %) 30 21 20 253 21

Thermodynamics for

CLC

+ ~ + + +

Kinetics/Reactivity2 – + + + –

Melting Points + ~ – + +

Strength + – ~ ~ ~

Environmental& Health ~ – – ~ –

Hydrogen Production + – – – –

1. Maximum theoretical oxygen carrying capacity; 2. Reactivity with CH4; 3. Mn3O4 is the highest oxidation state based on thermodynamics, although not thermodynamically favorable, Mn is assumed to be the lowest oxidation state

Structures of Iron Oxide

NaCl Type

oxygen close-packed

cubic pattern

iron occupy all

octahedral interstices

inverse Spinel Type

FeO Fe3O4

octahedral interstices

1/2 occupation rate

tetrahedral interstices

1/8 occupation rate

20

Pellet Reaction Mechanism – Ionic

Diffusion for Unsupported Iron

21

Partially oxidized Fe with support Pt mapping

Pt Epoxy Resin PtPellet bulk phase

Pellet Reaction Mechanism – Ionic

Diffusion for Supported Iron

Role of Support – Oxidation of Fe and Fe/TiO2Simulation

Energy barrier for O2- can be reduced after support addition

Oxygen anion transfer in Wüstite and Ilemnite

Modes of CFB Chemical Looping Reactor SystemsMode 1- reducer: fluidized bed or co-current gas-solid (OC) flows

Mode 2 - reducer: gas-solid (OC) counter-current dense phase/moving bed flows

Zone 2

Enhancing Gas

Fe

Coal/biomass

Fe2O3CO2/H2O

Zone 1 Zone 1

Zone 2

Zone 3

Zone 4

Coal/biomass

Thomas, T., L.-S. Fan, P. Gupta, and L. G. Velazquez-Vargas, “Combustion Looping Using Composite Oxygen Carriers” U.S. Patent No. 7,767,191 (2010, priority date 2003)

Chalmers University 10-kWth CLC System

Fluidized Bed Reducer

Contercurrent Gas-Solid(OC)

Reducer

fuel/reducing gas

air

Reducer

fuel reaction products

combustor gas

OC

OC

combustor gas

OC

Riser combustor

combustor gas

fuel reaction products

fuel/reducing gas

Reducer

air

OC

combustor gas

OC

OC

Riser combustor

Design Variation from Mode 1 to Mode 2

Original VUT 120-kWth CLC System (2007)

Modified VUT 120-kWth CLC System (2010)

25

Chemical Looping Reactor Design

FeOy

FeOx

CO/H2

CO2/H2O

(x>y)

FeOy CO/H2

(x>y)

FeOx CO2/H2O

Fluidized BedMoving Bed

FeOy CO/H2

(X>Y)

FeOx CO2/H2O

Fluidized Bed Moving Bed

Moving Bed – The Selected Reactor Type

FeOy

FeOx

CO/H2

CO2/H2O

(X>Y)

Fluidized Bed v.s. Moving Bed

Maximum Solid Conversion

Gas Velocity

Particle Size

11.11%

> Umfv

Small

50.00%

< Umfv

Large

Fluidized Bed v.s. Moving Bed

Maximum Solid Conversion

Gas Velocity

Particle Size

11.11%

> Umfv

Small

50.00%

< Umfv

Large

Maximum Solid Conversion

Gas Velocity

Particle Size

11.11%

> Umfv

Small

50.00%

< Umfv

Large

1.E-01

1.E+00

1.E+01

1.E+02

1.E+03

1.E+04

1.E+05

1.E+06

1.E+07

200 400 600 800 1000

Temperature (C)

PC

O2/P

CO

Fe2O3

Fe3O4

FeO

Fe

1.E-01

1.E+00

1.E+01

1.E+02

1.E+03

1.E+04

1.E+05

1.E+06

1.E+07

200 400 600 800 1000

Temperature (C)

PC

O2/P

CO

Fe2O3

Fe3O4

FeO

Fe

Fluidized Bed

Moving Bed

(x>y)

26

Particle Type Ni Cu Fe

Type of Data

Lab

Scale

CFB 120

kW

Lab

Scale CFB 10kW Lab Scale

CFB

300W

Moving Bed -H2

25 kW

Particle Type

NiO/

MgAl2O4

NiO/

MgAl2O4

CuO/

Al2O3 CuO/Al2O3

Fe2O3/

MgAl2O4

Fe2O3/

Al2O3 Composite Fe2O3

Air Flow Rate @1000 MWth and 10% Excess (mol/s) 11784 1309

Volumetric Air Flow Rate at 1 atm and 900 ºC (m3/s) 1134 126

Particle Circulation Rate @ 1000 MWth (kg/s) 4000 10000 3000 6000 8000 10000 800

Reducer Solids Inventory (tonne) 230 160 70total

2100

500 12001500 Total

Oxidizer Solids Inventory (tonne) 390 80 390 n/a 350

Medium Particle Size (μm) 153 120 300 200 153 151 2000

Particle Density (g/cm3) 1.9 5 2.5 2.5 4.1 2.15 2.5

Ut (m/s) 2 0.8 2 1.2 1.1 0.6 11

Uc (m/s) 4 4.8 4.9 4.2 4.8 3.6 4

Use (m/s) 6 6.7 7.5 6.1 6.9 4.9 9.7

Typical Riser Superficial Gas Velocity (m/s) 7.00 12

Bed Area Turbulent Section (if Required) at 1 atm (m2) 231.47 25.18

Bed Area Required for Riser Section at 1 atm (m2) 162.03 10.49

Corresponding Riser Diameter (m) 14.37 3.66

Solids Flux at 1 atm (kg/m2s) 24.69 61.72 18.52 37.03 49.37 61.72 76.23

Number of Beds Needed given 8 m ID Riser 3.23 <1

Number of Beds Needed given 1.5 m ID Riser 91.73 5.94

Ug for a Single 1.5 m ID Riser at 1 atm (m/s) 642.14 71.29

Ug for a Single 8 m ID riser at 1 atm (m/s) 22.58 2.5 (Ug < Ut; N/A)

Required Pressure for a Single 1.5m ID Riser (atm) 91.73 10.00

Solids Flux for a Single 1.5 m ID Riser (kg/m2s) 2264.69 5661.71 1699 3397.03 4529.37 5661.71 452.88

Required Pressure for a Single 8 m ID Riser (atm) 3.23Ug < Ut; N/A

Solids Flux for a Single 8 m ID Riser (kg/m2s) 79.62 199.04 59.71 119.43 159.24 199.04

4000 – 10000 kg/s or 14,000 – 36,000 ton/hour

< 3,000 ton/hour

27

Single Loop High Density CFB System (Kirbas et al., 2007)

Two Loop High Density CFB System (Kulah et al., 2008)

Kirbas G, Kim SW, Bi X, Lim J, Grace JR. Radial Distribution of Local Concentration Weighted Particle Velocities in High Density Circulating Fluidized Beds. Paper presented at: The 12th International Conference on Fluidization - New Horizons in Fluidization Engineering; May 13-17, 2007; Vancouver, Canada.

Kulah G, Song X, Bi HT, Lim CJ, Grace JR. A NOVEL SYSTEM FOR MEASURING SOLIDS DISPERSION IN CIRCULATING FLUIDIZED BEDS. Paper presented at: 9th International Conference on Circulating Fluidized Beds; May, 13 – 16, 2008; Hamburg, Germany.

Circulating Fluidized Bed Systems

Particle Fixed Bed Tests

Bench Scale Tests

Time

Sca

le

Sub-Pilot SCL

Integrated Tests

0

5

10

15

20

25

30

35

40

45

50

0 5 10 15 20 25 30 35

Axil Position (inch)

So

lid

Co

nv

ers

ion

(%

)

0

10

20

30

40

50

60

70

80

90

100

Gas C

on

vers

ion

s (

%)

Solid H2 COParticle Reactivity Confirmed

Maximum Operating Temperature Determined

Reactor Performance Confirmed

OSU Syngas Chemical Looping Process Development

Consolidation and Yield of Bulk Solids

0c

c

fff

: flowability of bulk solids

Flow Properties of Bulk Solids

Stress of Bulk Solids in Vertical Reactor

1

2

1 sin

1 sin

Flowing Condition

Arching Condition

1 2

1 sin

1 sincf

Piling of Bulk SolidsStress Condition of Bulk Solids

fc

Stress Distribution in Flowing Solids

lift upwardW F F

2

0 sW R h g 1 2( )sin 2liftF R h 2

support 0 2F R

22

0

2sin sin 2

(1 sin )s

dg

R dh

2 0( ) ahb b e

0

0

2sin sin 2

(1 sin )

(1 sin )

2sin sin 2s

aR

Rb g

1 2 1 2sin sin 2 (1 sin cos 2 ) tan2 2

xy

sinsin(2 ) sin

sin

2

v

v

Limitation from wall: fully developed wall angle

With counter-current interstitial gas flowDrag force can be treated as a reduction of gravity

0 (1 sin )

2sin sin 2s D

Rb g F

: angle of friction between the powder and the wall

σ0: external normal stress at the top of the solid surface

Stress Distribution in Arched Solids

' min( , / 4) Limiting Condition: Maximum lift force

' 21 2( )sin 2s

dg

dh

2 0( ) ahb b e '

0

0

'

2sin sin 2

(1 sin )

(1 sin ) (1 sin )

2sin sin 2 2sin

cs

aR

R fb g

Requirement for arching: 2 0

With counter-current interstitial gas flow: 0

'

(1 sin ) (1 sin )

2sin sin 2 2sin

cs D

R fb g F

Reactor Size Criteria for Arching

• No External Stress on Top

2 (1 )ahb e

0

'

(1 sin ) (1 sin )0

2sin sin 2 2sin

cs

R fb g

'

0

sin 2c

s

fR

g

Influence of Some Critical Parameters

1. Gas Flow

Counter-Current Interstitial gas flow causes reduction of gravity, and thus needs a larger reactor size

''

0 0

sin 2c

s D

fR R

g F

2. Particle Size

Smaller particles need larger reactor size

unconfined yield strength of some alumina-powders (*)

*: Kohler, T. and H. Schubert, Influence of the Particle-Size Distribution on the Flow Behavior of Fine Powders. Particle & Particle Systems Characterization, 1991. 8(2): p. 101-104

'

0

sin 2

1

c

s

c n

p

fR

g

fd

3. Mixing with Fine Powders

The flowability governed by flow properties of the fine powders as shearing takes place across the fines.

4. Layer of Fine Powders

'

' ' '

0

1ln

bh

a b

h

H0

Arching Criteria:

depend on height of fine powder layerσ1

kPa

European Chemical Looping Reforming/Gasification Application - I

Reducer:MeO + CH4 Me + CO + 2H2

Oxidizer:Me + O2 MeO

Overall Reaction:CH4 + 1/2O2 CO + 2H2

Juan adanez, International Journal of Hydrogen energy, 2011

European Chemical Reforming/Gasification Application - II

Ryden, M., and A. Lyngfelt, International Journal of Hydrogen energy, 2006

37

OSU Chemical Looping Integrated with Fuel Cell Application – 3

2H2 + O2 2H2O + Electricity

C + H2O/O2 H2 + CO2/Heat

Re

ac

tor 1Biomass

Sequestrable

CO2 and H2O

MeOx

An

od

e

Cath

od

e

H2 rich gasS

OF

C

Steam rich exhaust to Reactor 2

Compressed Air

Oxygen lean air

to Reactor 3

Oxygen lean air

from SOFC

cathode (Optional)

Re

ac

tor 3

Electric

Power

MeOy (y < x)MeOy (y < x)

MeOz

(y<z≤x)

Re

ac

tor 2

Re

ac

tor 1Biomass

Sequestrable

CO2 and H2O

MeOx

An

od

e

Cath

od

e

H2 rich gasS

OF

C

Steam rich exhaust to Reactor 2

Compressed Air

Oxygen lean air

to Reactor 3

Oxygen lean air

from SOFC

cathode (Optional)

Re

ac

tor 3

Electric

Power

MeOy (y < x)MeOy (y < x)

MeOz

(y<z≤x)

Re

ac

tor 2

38

OSU Syngas Chemical Looping in CTL Applications – II

Steam

from F-T

Biomass

and F-T

byproduct

MeOx

H2 rich gas

MeOy (y < x)

MeOz

(y<z≤x)Air (Optional)

F-T and

Product Upgrade

CO2

H2O

Sequestrable CO2

H2O

Liquid Fuel

Product

Byproduct to

Reactor 1

H2O

(Cooling)

Steam to

Reactor 2

Reac

tor 3

Reac

tor 1

Reac

tor 2

Steam

from F-T

Biomass

and F-T

byproduct

MeOx

H2 rich gas

MeOy (y < x)

MeOz

(y<z≤x)Air (Optional)

F-T and

Product Upgrade

CO2

H2O

Sequestrable CO2

H2O

Liquid Fuel

Product

Byproduct to

Reactor 1

H2O

(Cooling)

Steam to

Reactor 2

Reac

tor 3

Reac

tor 1

Reac

tor 2

3H2 + CO2 -(CH2)- + 2H2O

C + H2O/O2 H2 + CO2/Heat

39

Coal/

O2

Particulateremoval

H2S Removal

F-Treactor

Productseparation

Liquid Fuel

Gas

Phase

HRSG

H2

H2/CO = 0,5

H2 /CO=2

Gas

ifie

r

OSU Syngas Chemical Looping in CTL Applications – I

Fuel

Rea

ctor

H2

Rea

ctor

CO2

Air

N2

N2

Organization/Location Process Size Features

HUNOSA, Spain CaCO3 – CaO (CaOling)

looping for post combustion

CO2 capture

2 MWth CO2 is from the flue gas

generated from 50 MWe coal

power plant .

Technical University of

Darmstadt, Germany

CaCO3 – CaO (LISA)

looping for post combustion

CO2 capture

1 MWth Capture plant is an extension to

a 1052 MWe hard coal-fired

power plant; carbonator and

calciner both are CFBs.

Technical University of

Darmstadt, Germany

ECLAIR – ilmenite

Redox with coal for looping

combustion application

1 MWth Solid fuel conversion uses a

fluidized bed reducer operated

in a CFB looping system

Alstom, U.S. CaCO3 – CaO looping for

CO2 capture

/CaSO4 –CaS redox with

coal for looping combustion

application

3 MWth Process uses two calcium –

based loops in a chemical

looping system

OSU, U.S. Iron based oxygen carrier

redox with gaseous fuels for

H2 production in a Syngas

Chemical Looping (SCL)

gasification process

250 kWth High pressure SCL enables

high purity H2 generation and

high purity CO2 generation

using a countercurrent moving

bed reactor

Upcoming large-scale demonstrations of chemical looping technology

Concluding Remarks

• Chemical Looping embodies all elements of particle science and technology - particle synthesis, flow and contact mechanics, gas-solid reaction engineering…

• Success achieved in the operation of sub-pilot units reflect the likelihood of commercialization of this technology in the near future