Overview on the work carried out at the German Aerospace ...Steam and CO 2-Reforming of Natural Gas Steam reforming: H 2O + CH 4 3 H 2 + 1 CO CO 2 Reforming: CO 2 + CH 4 2 H 2 + 2

Solar Fuels

Overview on the work carried out at the German Aerospace Center

Dr. Christian [email protected]

www.DLR.de • Chart 1 Solar Fuels, Niigata University > 3 July 2012

Contents

- Short Introduction of the DLR- Energy Program- Institute of Solar Research- Department of Solar Chemical Engineering

- Solar Fuels- Short-term CO2-Reduction: Solar Reforming- Long-term: Water splitting processes

- Thermochemical Cycles- High Temperature Electrolysis

- Conclusion

Solar Fuels, Niigata University > 3 July 2012www.DLR.de • Chart 2

German Aerospace Center (DLR)


DLRGerman Aerospace Center

Research Institution Space Agency Project Management Agency


Research Areas

- Aeronautics- Space Research and Technology- Transport- Energy- Space Administration- Project Management Agency


Locations and employees

7000 employees across 32 institutes and facilities at

16 sites.

Offices in Brussels, Paris, Washington, Singapore, and Almería.

Permanent delegation on the European Solar Test Centre Plataforma Solar de Almería, Spain


Cologne

Oberpfaffenhofen

Braunschweig

Goettingen

Berlin

Bonn

Neustrelitz

Weilheim

Bremen Trauen

Lampoldshausen

Stuttgart

Stade

Augsburg

Hamburg

Juelich

Total income 2010 – Research, operations and management tasks (excluding trustee funding from the Space Administration / DLR Project Management Agency): € 745 Mio. (¥74 bn)

308

205

43

53

104

44 All values in € million

Space Research and Technology

Aeronautics

Transport

Energy

Space Administration / DLR Project Management Agency

Other income / earnings

> Standard presentation > Jan. 2012www.DLR.de • Chart 7

National and International Networking


World

Europe

Germany

Customers and partners: Governments and ministries, agencies and organisations, industry and commerce, science and research

Energy


DLR Energy

DLR Energy Research concentrates on: - CO2 avoidance by efficiency

optimisation and renewable energies

- synergies within the DLR- major research specific themes

that are relevant to the energy economy


Energy Program Themes

- Efficient and environmentally compatible fossil-fuel power stations(turbo machines, combustion chambers, heat exchangers)

- Solar thermal power plant technology, solar fuels

- Thermal and chemical energy storage

- High and low temperature fuel cells

- Systems analysis and technology assessment


Institute of Solar Research

Department of Solar Chemical Engineering



DLR Institute of Solar ResearchMain Topic:

Solar Thermal Power Plants

140 Persons

5 Departments, 4 Sites

Köln-Porz, Jülich

Stuttgart

Plataforma Solar de Almería(Permanent Delegation)

and Office in Almería, Spain

Köln-Porz

Stuttgart

Jülich

Department of Solar Chemical Engineering

www.DLR.de • Folie 14

HeadOrganisation

StrategyRepresentation in

boards

GroupHigh temperature CESolar tower >500°C

Solar FuelsSolar Materials

GroupLow temperature CE

Reactors up toParabolic troughs

< 500°C

Heat transfer fluidsSolar fuels

Water treatmentSOWΛRLΛ GmbH

Solar Fuels, Niigata University > 3 July 2012

25 Persons + Students, 65% external funding

Competences

Development ofcomponents andprocesses

and

scientific, technologic andeconomic evaluation

850 mm

530 mm 1000 mm

1373

1500000

06

314

1500000

25

CO2TOT

1073

1500000

25

CO-O2

973

1500000

20

CO

1073

1500000

5O2

500

1500000

20

1

298

1500000

4

N2TOT

1473

1500000

9

REGOUT

1373

1500000

9

5

413

100000

9

7

298

1500000

13

CO2

298

100000

12CO2-OUT

298

1500000

193

DEA 298

1500000

193DEATOT

309

1500000

9

CO-OUT

353

1500000

205

8

371

200000

16

10

422

200000

189

9

298

100000

4WATER

398

100000

193

DEAREC

298

100000

193

RECDEA

413

100000

5

O2,CO2

413

100000

4N2REC

298

1500000

4

N2

RECSPLT

Q=100000000

LOSS1

Q=-2484963

COOL1

Q=-10978344

RECREG

Q=8127743

LOSS2

Q=-1077572

COOL3

Q=-9381091

MIX1

MIX2

ABSORBER

QC=0QR=0

STRIPPER

QC=-21373997QR=87412428

FLASH

Q=-11238142

MIX3COOL4

Q=-58429041

SEP

Q=-1

MIX4Temp erature (K)

Pressure (N/sq m)

Mass Flow Rate (kg/sec)

Q Duty (Watt)

DEA

O2, CO 2

CO

www.DLR.de • Folie 15 Solar Fuels, Niigata University > 3 July 2012

Solar Fuels

> 20 years experience andinternational cooperation

Processes Reforming of NG Thermo-chemical cycles

Sulfur metal oxides

Solar HT electrolysis Cracking of methane Photo-catalysis

Products H2, syn-gas, methanol,

FT-Synfuels …

(Roeb, Müller-Steinhagen, Science, Aug. 2010.)

1200°C

800 – 1200 °C

- O2

H2O - O2- H2-MOred

-MOred-MOox

-MOox

Contact DLR: Dr. Martin Roeb, ([email protected] Tel.: +49(0)2203 601 2673)


H2

½ O2

Solar Materials

- High temperature recycling ofwaste materials (e.g. aluminium, sulfuric acid)

- Development of solar heatedreactors – solar heated rotary kilns

- Development and demonstration ofproduction processes


Contact DLR: Dr. Martin Roeb, [email protected]

Tel.: +49(0)2203 601 2673

Heat Transfer Fluids for CSP

- Accelerated AgingDegradation rates, and kinetics of gas, water, and other degradation productsformation

- Physico-chemical parameter at high temperaturesVapor pressure, density, heat capacity, heat conductivity, viscosity, gas soluability

- Interaction with power plant componentsHydrogen diffusion, influence of material contacts and impuritieson the aging ofthe heat transfer fluids

- Field testsAuthentic and representative samples of heat transfer fluids during power plant operation, inline- / atline- / offline-analysis

Contact DLR: Dr. Christian Jung ([email protected]; Tel. +49 (0) 2203 601 2940)


Photocatalytic Synthesis of Solar Fuels

- Qualification of new photo-catalysts for hydrogen production or thereduction of CO2

Determination of spectral quantum yields by special lamp technologies, Determination of the solar efficiency in our solar test fascilities, Evaluation of long term stability, and product quality, optimisation of theproduktivity

- Chemical EngineeringDevelopment of solar receiver-reactors, design of concentrator technologies, scale-up, and economic evaluation



Photochemical Water Treatment

- Untersuchung photochemischer Verfahren (VUV bis solar)Actinometry of light sources, degradation tetst by photolytic and photo-catalyticprocesses; water analytics

- Development of photo-reactorsSolar receiver-reactor technology and photo-reactors for nnovative light sources

- Development of photo-chemical plantsPlants for water treatment with photo-chemical key steps up to demonstrationscale, research on the combination of treatment technology, automation, recycling of photo-catalysts, energetic optimisation



Solar Fuels


Solar Chemistry - Basics

- Role models - photosynthesis - use of photons for photochemistry- burning glass – use of heat for thermochemistry

- Principle in chemical reactions: - photochemistry ≠ thermochemistry

- However in some cases there are synergies in chemical processes, especially if not only one reaction takes place

- Example: degradation of wastes

Slide 22 www.dlr.de/ Solar Fuels, Niigata University > 3 July 2012

Solar Chemistry instead of Solar Power

- Solar Thermochemistry is efficient because energy conversion steps arereduced!

- Example: Hydrogen production: H2O → H2 + ½ O2- Solarchemical: 2 conversions

- Solar radiation – heat – Chemical reaction- Via solar power: 4 conversions

- Solar radiation – heat – mechanical energy – electrical energy –chemical reaction

- Solar photo-chemistry uses the light directly without any conversion. Photo-chemistry is economical if the reaction needs a large amount ofphotons

- Example: Production of Caprolactam an intermediate for Nylon Annual production > 200,000 t (by artificial light)

Slide 23 www.dlr.de/ Solar Fuels, Niigata University > 3 July 2012

Solar Fuels – Production pathways

Slide 24 www.dlr.de/

Hydrogen

Fossil Resources Biomass PV

Radiation

Solar Energy

Power

Electrolysis PhotochemistryThermochemistry

Mechanical Energy

Heat

Heat

CO2

Synthetic Fuels

Solar-thermal

Solar Fuels, Niigata University > 3 July 2012

Temperature Levels of CSP Technologies

-Paraboloid: „Dish“

-Solar Tower (Central ReceiverSystem)

-Parabolic Trough / Linear Fresnel

3500°C

1500°C

390°C

150°C50°C


Solar Towers, “Central Receiver Systems”


-PS10, PSA CESA-1, Torresol, Spain -Solar-Two, Daggett, USA-Solarturm Jülich, Germany

Annual Efficiency of Solar Power TowersPower Tower 100MWth

Optical and thermal efficiency / Receiver-Temperature

0

5

10

15

20

25

30

35

40

45

50

600 700 800 900 1000 1100 1200 1300 1400

Receiver-Temperature [°C]

Opt

ical

effi

cien

cy a

nd th

erm

al a

nnua

l use

ef

ficie

ncy

[%]

R.Buck, A. Pfahl, DLR, 2007


Solar Tower Jülich


Receiver 22.7m²

(Intratec, Saint-Gobain)

Tower 60m

(Züblin)

2150 Heliostats á 8.2 m²

(SHP/AUSRA)

Vessel 9t/h, 30 bar/500°C

(VKK-Standardkessel)

Thermal storage 1h

Turbine 1.5 MWe

(KKK-Siemens)

Principle of the solar thermal fuel production

Solar Tower

HeatChemicalReactor

Fuel-H2-CO + H2

Energy Converter-Fuel Cell

-Transportation

-Power Production

Recourses-Natural Gas-Water, CO2

-Industry-Transportation


Short-term CO2-Reduction: Solar Reforming


CO2 Reduction by solar heating of state of the art processes like steam methane reforming and coal gasification

kg/k

g

SMR

SSMR

CG

SPCR

0

5

10

15

20

25

30

SMR SSMR CG SPCR

-CO2 Reduction 20 – 50%


Steam and CO2-Reforming of Natural Gas

Steam reforming: H2O + CH4 3 H2 + 1 CO

CO2 Reforming: CO2 + CH4 2 H2 + 2 CO

Reforming of mixtures of CO2/H2O is possible and common

Use of CO2 for methanol production:

e.g. 2H2 + CO CH3COH (Methanol)

Both technologies can be driven by solar energy as shown in the projects: CAESAR, ASTERIX, SOLASYS, SOLREF…


Solar Methane Reforming – Technologies

- Reformer heated externally (700 to 850°C)

- Optional heat storage (up to 24/7)

- E.g. ASTERIX project

- Irradiated reformer tubes (up to 850°C), temperature gradient

- Approx. 70 % Reformer-h- Development: CSIRO, Australia

and in Japan; Research in Germany and Israel

- Australian solar gas plant in preparation

- Catalytic active direct irradiated absorber

- Approx. 90 % Reformer-h- High solar flux, works only

by direct solar radiation- DLR coordinated projects:

Solasys, Solref; Research in Israel, Japan

decoupled/allothermal -indirect (tube reactor) Integrated, direct, volumetric

Source: DLR


Project Asterix: Allothermal Steam Reforming of Methan

- DLR, Steinmüller, CIEMAT- 180 kW plant at the Plataforma Solar de Almería, Spain

(1990)- Convective heated tube cracker as reformer- Tubular receiver for air heating


Pilot Scale Solar Chemical Reactors - SolarGasExperimental set-up of the 200 kW SolarGas reactor

Source: R. McNaughton et al., CSIRO, Australia

Top view of DCORE reactor (right) layout of entire integrated reformer and HRU


Direct heated volumetric receivers:SOLASYS, SOLREF (EU FP4, FP6)- Pressurised solar receiver,

- Developed by DLR- Tested at the Weizmann Institute of Science, Israel

- Power coupled into the process gas: 220 kWth and 400 kWth

- Reforming temperature: between 765°C and 1000°C

- Pressure: SOLASYS 9 bar, SOLREF 15 bar

- Methane Conversion:max. 78 % (= theor. balance)


Potential Solar sites


Suitable locations for CSP in Northern Africa


Natural Gas Pipeline Grid and Natural Gas Fields


Suitable locations for solar reforming - Example Algeria and Tunisia

- 50 km distance to pipelines- Acceptable DNI- Available Land

kWh/m²/y

-Pipelines -Fields


Long-term: Water splitting processes


Solar Pathways from Water or CO2 to Hydrogen


Carbon Monoxide


Carbon Monoxide



Promising and well researched Thermochemical CyclesSteps Maximum Temperature

(°C)LHV Efficiency

(%)

Sulphur CyclesHybrid Sulphur (Westinghouse, ISPRA Mark 11) 2 900 (1150 without

catalyst)43

Sulphur Iodine (General Atomics, ISPRA Mark 16) 3 900 (1150 without catalyst)

38

Volatile Metal Oxide CyclesZinc/Zinc Oxide 2 1800 45

Hybrid Cadmium 1600 42

Non-volatile Metal Oxide CyclesIron Oxide 2 2200 42

Cerium Oxide 2 2000 68

Ferrites 2 1100 – 1800 43

Low-Temperature CyclesHybrid Copper Chlorine 4 530 39


45

Efficiency comparison for solar hydrogen production from water (SANDIA, 2008)*

Process T[°C]

Solar plant Solar-receiver+ power [MWth]

η T/C

(HHV)

η Optical η Receiver

ηAnnual

EfficiencySolar – H2

Elctrolysis (+solar-thermal power)

NA Actual Solar tower

Molten Salt 700

30% 57% 83% 14%

High temperature steam electrolysis

850 Future Solar tower

Particle 700

45% 57% 76,2% 20%

Hybrid Sulfur-process


Particle 700

51% 57% 76% 22%

Hybrid Copper Chlorine-process


Molten Salt700

49% 57% 83% 23%

Nickel Manganese Ferrit Process

1800 Future Solar dish

Rotating Disc < 1

52% 77% 62% 25%

*G.J. Kolb, R.B. Diver SAND 2008-1900

H2

H2O

O

O

O

OH

HOH

HH

H

O H

HMOreduced MOoxidized

MOreduced MOoxidized

Fuel Production from H2O and CO2 by Solar Radiation

1200 °C

800-900 °C

DLR: Roeb, Müller-Steinhagen, Science, Aug. 2010

CO2

CO


2004:

First solar thermochemical

Η2 production

2008:

Pilot reactor (100 kW)

2005:

Continuous Η2 production

Hydrosol technology scale-up

DLR solar furnace

PSA solar tower


Pilot-plant in operation since March 2008


Modelling-ControlSoftware(Labview®)

Hydrogen ProductionModel

Modelling of the pilot plant - Overview Modelling:

TemperatureModel(Matlab/Simulink®)

Heliostatfield-Simulation ToolSTRAL (C++)Insulated Power (#1)

Parameter

Parameter

Temperature (#2)

Parameter

Hydrogen Amount (#3)



Modelling – Temperature model:

KFQ aKQ

Collecting formulas of the heat flows (simplified balance!)

Heat flows: heat radiation, heat conduction and convection

HSQaFQ

KFQ

aKQ

KKQ

GaBaQKGaQ

aFQ

GBQ

Modelling – Temperature model:

First Verification of open loop control system

Temperatures East (23.04.2009)

0

200

400

600

800

1000

1200

1400

10:15

:0010

:30:00

10:45

:0011

:00:00

11:15

:0011

:30:00

11:45

:0012

:00:00

12:15

:0012

:30:00

12:45

:0013

:00:00

13:15

:0013

:30:00

13:45

:0014

:00:00

14:15

:0014

:30:00

14:45

:0015

:00:00

Time

T [°

C]

Temperature SimulatedTemperature Measured

Regeneration

Production

Input:

Simulated power East

Sampling rate (Sim.):

every second

Sampling rate (Exp.):

Every second

Average Deviation: 6.5%


Pilot Plant arranged on the research platform of the ST Jülich (artist view)

Solar Fuels, Niigata University > 3 July 2012Solar Fuels, Niigata University > 3 July 2012www.DLR.de • Chart 52


Carbon Monoxide


Sulphur-Iodine Process

Water

H2OOxygen

O2Heat

800–900 °C

Hydrogen

H2

The thermochemical cycles covered in HycycleS

Electrolysis (90°C) HH22SOSO44 + H+ H2 2 SOSO22 + 2 H+ 2 H22O O

HH22HH22OO

OO22

HH22SOSO44

SOSO22

WWäärmerme

800800°°C C –– 12001200°°CC

HH22SOSO44 HH22O + SOO + SO33SOSO33 SOSO22 + + ½½OO22

+ H+ H22OO

HH22SOSO44 + H+ H2 2 SOSO22 + 2 H+ 2 H22O O

HH22HH22OO

OO22

HH22SOSO44

SOSO22

800800°°C C –– 12001200°°CC


+ H+ H22OO

HeatHeat

Electrolysis (90°C) HH22SOSO44 + H+ H2 2 SOSO22 + 2 H+ 2 H22O O

HH22HH22OO

OO22

HH22SOSO44

SOSO22

WWäärmerme

800800°°C C –– 12001200°°CC


+ H+ H22OO

HH22SOSO44 + H+ H2 2 SOSO22 + 2 H+ 2 H22O O

HH22HH22OO

OO22

HH22SOSO44

SOSO22

800800°°C C –– 12001200°°CC


+ H+ H22OO

HeatHeat

Hybrid Sulphur Cycle


H2SO4 decomposition in 2 steps

1. Evaporation of liquid sulfuric acid (400°C)

-SiSiC foam

-SiSiC honeycomb

-Absorbers:

-2. Dissociation of sulfur trioxide (850°C)


Performance of long-term corrosion campaigns (SO2, SO3 rich, boiling H2SO4) and post-exposure mechanical testing and inspection

mainstream materials SiC-based as well as brazed samples SiC based materials retained suitable for the intended application since they are not

affected significantly by the SO2-rich, SO3-rich and boiling sulphuric acid exposures.

Stability of construction materials

High temperature

tests (850oC)

SiO2layer

Core material

0 200 400 600 800 1000300

350

400

450

500

Ebe

ndin

g (G

Pa)

Exposure time (hrs)

CEA1


‘In-house’ synthesized materials (metal oxide based) with high catalytic activity interms of SO2 production from H2SO4:

Coating of active materials in small- & large-scale SiSiC monoliths or fragments

Satisfying stability of samples coated with ‘in-house’ materials under ‘long-term’operation

Derivation of an empirical kinetic model

Evaluation of the employed materials chemical stability Extraction of an SO3 dissociation mechanism CrFe oxide identified as the most suitable catalyst

Advanced catalysts and coatings for H2SO4 decomposition

0

10

20

30

40

50

60

70

80

90

100

8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0

WHSV (h-1)

SO3

conv

ersi

on (%

)

exp. 1 bar

exp. 2 bar

exp. 3 bar

exp. 4 bar

kin model 1-4 bar

Karagianakis et al, IJHE 2011/2012; Giaconia et al, IJHE 2011



CuAl2O4‐coated SiSiC fragments (kinetic model for decomposer design)

Exp. campaign Ea (kJ/mol) A (h‐1) dn (mm)*

No. 1 240.3 5.6*1012 1‐4

Example of Catalyst qualification: CuAl2O4

WHSVkX )1ln(

RTEa

eAk

0102030405060708090

775 800 825 850 875 900

SO3 conversion

(%)

temperature (°C)

40 h‐1 63 h‐1

128 h‐1

290 h‐1

equilibrium

0

10

20

30

40

50

60

70

0 20 40 60 80 100 120 140 160

SO3 conversion

(%)

time on stream (hours)

850°C, WHSV= 290 h‐1

Durability tests performed at “high” space velocity values After initial deactivation, catalyst shows < 5% loss of activity (100hrs on stream) Change of colour observed, due to phase separation phenomena


Design of multi-chamber solar reactor

Front view of evaporator (left) and decomposer

Rear view

H2SO4

SO3 + H2O

SO2 + O2 + H2OSolar radiation(focus 2)

Solar radiation(focus 1) honeycomb

foam

Solar reactor for sulfuric acid decomposition

H2SO4 SO3 + H2O

SO3 SO2 + ½ O2

850°C

400°C

750°C 650°C


Operation in our solar furnace in Cologne

Overview of test series in solar furnace

Catalyst Fe2Cr2O4

Evaporator solar

Number of experiments 19

Sulfuric acid concentration w% 94

Sulfuric acid flow rate ml/min 1…8

Mean honeycomb temperature °C 650…850

Residence time s 0.3…1

Weight hourly space velocity 1/h 0.6…4.7


Thermodynamic equilibrium of H2SO4 decomposition

H2SO4 dissociation completed at about 550°C

80% of SO3 decomposed at 850°C

40% of SO3 decomposed at 650°C

Source: Noglik et al., 2009


Conversion of SO3 in honeycomb



Solar reactor as H2SO4 decomposer

- Development and operation of a scalable prototype

- FEM analysis- trouble-free operational > 200 h- conversions > 80 %- reactor efficiency > 25 %

- Continuum model of foam vaporiser- Computer tomography

- Modelling of SO3 decomposition- Validation with experimental

data- Control procedure for scale-up solar

tower system

0 1 2 3 4 5 6 70

10

20

30

reactor (Fe2O3 catalyst) net (Fe2O3 catalyst)

[%

]

Vacid [ml/min]

Thomey et al, IJHE 2012

Noglik et al, IJER 2010

Haussener et al, ASME-JHT 2009

Scale-up of the solar HyS process


Implementation into a Solar Tower


Techno-economics

Flowsheet for solar HyS process refined and completed

All Components including the solar field were sized for a nuclear HyS and SI process and a solar HyS process

Investment, O&M cost, production cost were analysed 6-7 €/kg(H2) for HyS optimistic scenarios lead to 3.5 €/kg(H2)

50 MW solar tower plant for hydrogen production by HyS cycle defined and depicted

Thorough safety analysis was carried out for respective nuclear and solar power plants

By-product revenues

Decomposer investment

Plant life

Electrolyser investment

Discount rate

Electricity cost

Electrolyser replacement

6 8 10 12Production cost of hydrogen [€/kg]

Start-up expenses

InterestsPeriphery

StorageGeneral facilities

Contingencies


50%26%

4%

5%

Equipment


Contingencies

General facilities

Storage

Periphery (Land & Piping)

Interests

Start-up expenses

9%2%

2%

2%

Equipment

Lebros et et al, IJHE 2010



Carbon Monoxide


High temperature electrolysis processTemperature in the range of 600°C to 900°C are required to drive the electrolyser.Electricity and heat are supplied to the electrolyser to drive the electro-chemicals reactions. The waste heat from the H2 and O2 gas streams existing the cell is used to evaporate water.The H2O stream is further heated by the second Heat exchanger to raise the temperature of the electrolyser.

222 2 OHeOH

eOO 221

22

222 21 OHOH


Economic analysis

Key parameters of the hydrogen production cost with the a concentrating solar installation coupled to a high temperature electrolyser:

Efficiency of the plant

Efficiency of the solar installation

Electricity consumption of the electrolyser

Site of the plant (annual solar irradiation, availability of water, connection to the electricity and gas grit

Investment

Lifetime of the plant


Thermal conductivity of working fluids


Flow diagram of the coupling of the solar power tower with the electrolyser


Flow diagram of the coupling of the parabolic dish to the electrolyser


Flow Diagram of the coupling of the parabolic trough to the electrolyser

Feed Water

Sensible heat storagefor pre-heating

Latent heat storagefor evaporation

Sensible heat storagefor super-heating

Power Block

ElectrolyserBlock

Parabolic Trough Collectors

Pre-heating Evaporation Super-heating


Conclusion and Outlook


Future Solar Thermal Plants – more than power!

Production of solar fuels (renewable H2 and CH4 / CH3OH),Recycling of CO2, Power Production and Desalination (H2O)

CO2

H2O

Sea water

Desalinated Water

CH4, CH3OH

H2

Heat

Power

• Solar Fuels, Niigata University > 3 July 2012• www.DLR.de • Chart 77

Acknowledgement- Thanks to all our funding agencies especially the

European Commission and our industrialpartners.

- Thanks to all colleagues and partners whoprovided various contributions to this work.


DLR H2 AircraftANTARES

Thank you very much for your attention!


Documents

Overview on the work carried out at the German Aerospace ...Steam and CO 2-Reforming of Natural Gas Steam reforming: H 2O + CH 4 3 H 2 + 1 CO CO 2 Reforming: CO 2 + CH 4 2 H 2 + 2