Revankar-1

A Seminar Presented at

Shripad T. Revankar

School of Nuclear Engineering, Purdue University, USA

Division of Advanced nuclear Engineering, POSTECH, South Korea

Department of Mechanical Engineering, IIT Bombay India

Department of Energy Science and Engineering

Indian Institute of Technology Bombay

April 6, 2016

Technologies for Hydrogen Economy

Revankar-2

Outline The World Energy Picture and Issues

Hydrogen Economy

Challenges and Opportunities

Hydrogen Production Photolysis H2

Bio-catalysts H2

Thermochemical H2

Hydrogen Storage Chemical Storage

Hydrogen Conversion

Conclusions

Revankar-3

Humanity’s Top Ten Problems for next 50 years

1. ENERGY

2. WATER

3. FOOD

4. ENVIRONMENT

5. POVERTY

6. TERRORISM & WAR

7. DISEASE

8. EDUCATION

9. DEMOCRACY

10. POPULATION

2012 7 Billion People

2050 8-10 Billion People

Source: R. E. Smalley, Rice University,

2004,Presented at Purdue University

Source: United Nations, Department of Economic and Social Affairs, Population Division (2011): World

Population Prospects, the 2010 Revision. New York

Revankar-4

World Population Density and Growth

Source: United Nations, Department of

Economic and Social Affairs, Population

Division (2011). World Population 2010

(Wall Chart). ST/ESA/SER.A/307.

http://static.ddmcdn.com/gif/maps/pdf/

WOR_THEM_PopDensity.pdf

Revankar-5

Global Energy Resources

Source: United Nations, Department of Economic and

Social Affairs, Population Division (2011). World

Population 2010 (Wall Chart). ST/ESA/SER.A/307.

Source: National Petroleum Council, 2007 after Craig, Cunningham and Saigo

Revankar-6

Source: Energy Information Administration / Annual Energy Outlook 2008

World Primary Energy Consumption by Fuel Type Q

uadra

illio

n B

tU

Quadrillion BtU (1015 BTU), = Exajoule (1.055 × 1018 J)

Revankar-7

Energy Supplies –Demand, Oil Example

Source: National Petroleum Council 2007

Source: Energy Information Administration /

Annual Energy Outlook 2008

Revankar-8

World Energy Supplies: One Vision

1900 1900 1920 1920 1940 1940 1960 1960 1980 1980 2000 2000 2020 2020 2040 2040 2060 2060 2080 2080 2100

20 20

40 40

60 60

80 80

100 100 100 BILLION

BARRELS

Per Year

Billion

Barrels

of Oil

Equivalent

(GBOE)

Gas Natural

Hydroelectric

Crude Oil

Solar , Wind Geothermal

Nuclear Electric

1993

Coal Coal

Decre

asin

g

Fossil F

uels

N

ew

Te

ch

no

log

ies

World Energy Demand

after Edwards,

AAPG 8/97

Historical Projected

Revankar-9 Source: Energy Information Administration / Annual Energy Outlook 2010

World Primary Energy Consumption by Fuel Type Q

uadra

illio

n B

tU

Revankar-10 Source: EIA, International Energy Outlook 2010

World Energy Flow Map

Source: EIA, International

Energy Outlook 2010

Qu

adra

illi

on

B

tU

Quadrillion BtU (1015 BTU), = Exajoule (1.055 × 1018 J)

Revankar-11 11

Source: EIA, International Energy Outlook 2004

World Green House Gas Emissions

Source: EIA, International

Energy Outlook 2010

Qu

adra

illi

on

B

tU

Quadrillion BtU (1015 BTU), = Exajoule (1.055 × 1018 J)

Revankar-12

Environmental Issues • CO2 Buildup

• Global Temperature

• Pollution

NOAA/NGDC Paleoclimatology Program

Revankar-13

Best investment potential in terms of

• Petroleum diesel

• Gasoline

• Biodiesel

• Ethanol

• Hydrogen

• Electrical

• But electricity is not suitable for all of our fuel requirements

Hydrogen as Energy Carrier

Reduced Emission

Carbon Free Cycle

Expands domestic sources

Energy Security

Energy Diversification

Different Sources

Hydrogen (H2)

Green Fuel

Revankar-14

Why do we need it as an alternative fuel?

• Environment

Global warming, local urban air quality

• Energy reserves

Increasing consumption vs. decreasing reserves

• Global political

Energy security and energy access, independency

• Hydrogen value proposition

New technology for transportation, clean conversion

H2 Can be produced from

• Renewables –solar, wind, biomass, wave

• Any fossil fuel

• Nuclear energy

Hydrogen as Energy Carrier

Revankar-15 Source: IIASA, Nakicenovic

102

101

100

10-1

10-2

Rati

o o

f H

yd

rog

en

(H

) to

Carb

on

(C

)

1800 1850 1900 1950 2000 2050 2100

0.90

0.80

0.67

0.50

0.09

H / (

H+

C)

Wood: H/C = 0.1

Methane: H/C = 4

Oil: H/C = 2

Coal: H/C = 1

t = 300 years (length of process)

1935 (midpoint of process)

Methane Economy

Hydrogen Economy

Non-Fossil Hydrogen

Ratio of hydrogen to carbon

Revankar-16

Vision for the Hydrogen Economy

“Hydrogen is America’s

clean energy choice.

Hydrogen is flexible,

affordable, safe, domestically

produced, used in all sectors

of the economy, and in all

regions of the country.”

Available at: www.eren.doe.gov/hydrogen/

Revankar-17 Revankar 17

Characteristics of the H2 Economy

Buildings use hydrogen for heat and power

Vehicles are powered by hydrogen and are integrated with

the heat and power system for homes, offices, and factories

Hydrogen is produced economically from sources that

release no carbon dioxide

The distribution infrastructure is well developed

Storage and use of hydrogen is safe

Revankar-18

Challenges and Opportunities

Solar / biomass

Electricity

Petroleum

Natural Gas

Coal

• Production

• Storage method

• CO2 Stabilization

• Cost

• Transportation Method

• Infrastructure Development

• Codes & Standards

• Hydrogen Delivery Cost

Car makers Government, Energy Suppliers

Hydrogenated

compounds Hydrogen

Production Delivery, Supply Usage/Application

Iss

ue

s

Iss

ue

s

Iss

ue

s • Stack Durability

• Power Density

• Freeze Start Capability

• Driving Range

• Vehicle Cost

Nuclear

Revankar-19

Hydrogen Production

World Production 50 Million Tons/year

• Equivalent to 2% of current world energy demand (if used in fuel cell)

• 12 million tons of hydrogen are currently produced by US each year

Hydrogen Sources

• Natural Gas Reforming (over 80%) CH4 +H2O CO + 3H2 -Reformation

CO+H2O CO2 + H2 - Shift

• By-Product Recovery (20%)

About 95% is produced for use in

• Ammonia

• Oil Refining • Methanol

Revankar-20 20

Hydrogen Production Methods Method Of Hydrogen

Production Inefficiencies

Electrolysis Requires electricity, expensive

Thermo-chemical water splitting

Requires outside energy and storage

Photolysis (photoelectrochemical processes)

sunlight as the input energy, storage,

Biological & photobiological (sunlight-assisted) water splitting

These methods are still in experimental stages

Thermal water splitting organic compounds release pollutants into the earths atmosphere.

By-product of petroleum refining and chemical production

Detrimental environmental and health problems this process may cause.

Revankar-21

Timing of R&D for Hydrogen

production technology

Revankar-21

Revankar-22

Production: Challenges

Revankar-23

Scientific Challenges and Opportunities

New materials for photo-catalysts Cost/efficiency (duty cycle) for solar thermo-chemical (TC)

Separations and materials performance

H2 from direct thermolysis (>2500oC) and radiolysis

Thermodynamic data and modeling for TC

High temperature materials in oxidizing environments at ~900oC

- Solid oxide materials and membranes

- TC heat exchanger materials

High temperature gas separation

Improved catalysts for reactions

Production: Nuclear and Solar Hydrogen

Revankar-24

Nuclear Hydrogen Technology: Thermochemical Cycles (TC)

1/2O2+SO2 + H2O SO2+2H2O+I2 I2 + H2

2HI H2SO4

SO2

H2

O2

H2O

I2

H2SO4 H2SO4 + 2HI 2HI

850-950 °C 1/2O2+SO2 + H2O SO2+2H2O

H2SO4

SO2

H2

O2

H2O

H2SO4 H2SO4 +H2

850-950 °C

SRNL Sandia

Labs

Hybrid-Sulfur

(1) H2SO4 H2O + SO2 + 1/2O2

(2) 2H2O + SO2 H2SO4 + H2

Sulfur Iodine

(1) H2SO4 H2O + SO2 + 1/2O2

(2) 2HI I2 + H2

(3) 2H2O + SO2 + I2 H2SO4 + 2HI

TC cycles require high temperatures, extensive thermal management, and cycle optimization

Revankar-25 25

Modeling Studies: Coupled H2-HTR System

Generation IV Initiative

and Nuclear Hydrogen

Initiative

Use nuclear

heat to drive

highly

endothermic

chemical

process

plants

Revankar-26

HTR Energy Conversion

• Electrical generation - Gen IV Energy Conversion Program

• Hydrogen production - Nuclear Hydrogen Initiative (NHI)

300 400 500 600 800 900 1000 1100

SFR

SCWR

MSR

Ca - Br

700 Temp C

VHTR

GFR

Pb FR

S-I, HyS

K-Bi

- Hydrogen Production

Temperature Ranges

Hydrogen Production

Temperature Ranges

Gen IV Reactor Output

Temperature Ranges

Mg-I

HyCu-Cl

HTE [with heat recuperation]

HT

R

Th

erm

o-c

hem

Pro

c.

Revankar-27

Fuel Performance Modeling

Fuel Studies

Fuel and Materials

Irradiation

Post Irradiation

Examination &

Safety Testing

• Coated Particle Fuel

and irradiation

• Analysis Methods

Development &

Validation Structural

• Graphite Development

• Material Properties

Emerging Technologies in High Temperature

Gas Cooled Reactor High thermal efficiency

Whole Core

Modeling

Ni from Watts

bath plating Cr Oxide

surface layer Al Oxide

intergrowth

Material

Characterization

Revankar-28

New high temperature reactor systems

Efficient and stable catalytic decomposition of HI and SO3

Develop flowsheet analysis of the SI cycle with advances techniques

Develop models for coupled system VHTR and SI cycle H2 plant,

- Catalyst development

- Design catalytic reaction conditions

- Catalyst characterization

- Evaluation of catalyst activation

Optimized Flowsheet for SI Cycle and Hy S Cycle

N2

MFC

Detector

HI 57% w/w

or H2SO4

Catalyst Reactor

Trap1 Trap2 Silica gel

SEM image of

Catalyst

System of catalyst reaction

SI Cycle Hy-S Cycle

Chemical process plant

simulation using data from

Prof. Lee’s group

Dynamic modeling with

reactor kinetics and

thermal-hydraulics models

for the couple system

Temperature

distribution in

PBMR core

Rea

cto

r c

ore

po

we

r fl

ux

Integrated VHTR & SI Cycle Hydrogen Plant Analysis

Emerging Technologies in Nuclear Hydrogen Generation

Revankar-29 29

SI-Thermochemical cycle

Extensive literature review of 70+ TC cycles:

1. Sulfur Iodine (SI) Cycle

2. Hybrid Sulfur (HyS) Cycle

SI cycle was developed and flow-sheeted by General Atomics in the 1970s

Paul Pickard, 2009

Integrated SI loops: 1980s GA, (US) 2004 JAERI, (Japan) 2009 INERI (DOE/CEA), (France) 2010 Tshingua (China) 2011 KAERI-KIER-RIST-POSTECH

Separate Effects Tests

GA, SNL, CEA, JAERI, KAIST, POSTECH

Revankar-30

GA-CEA-SNL Sulfur-iodine

Integrated Laboratory Scale Demonstration

Revankar-30

SECTION I SECTION II

SECTION III

Boiler

Superheater

Decomposer

Interface Skid

HI Decomposer

Bunsen Reactor

Revankar-31

Chemical plant

Modeling Work

31

Chemical

kinetics

models (literature)

Transient

reaction

chamber

model (thermo-

dynamics)

Steady state

reactant

concentrations (ASPENPlus

flowsheets)

Nuclear plant

Thermal

hydraulic

model

(THERMIX-

DIREKT)

Neutron flux

shape functions (3D PARCS-

THERMIX)

Point

kinetics

model (literature)

IHX

Chemical Flowsheet Analytical Model System Codes

Revankar-32

Section I- If the inlet stream of S-101 is disconnected to the outlet stream of the

Bunsen reactor (116), and appropriate inlet flow condition is specified

for S-101, converges

118B

119B

129

139

138

110

130A

C-103-2

C-103-3

C-103-4

C-103-5

C-103-1

140

132A

C102

C104

C103-R1

C103-R2

C103-S1

C103-S2

R101

S101

C101

MIX-115

115 116

119A

118A

117A

117B

111

113

132B

137B

121

120

101B

102B

106B

FS105

P102

103

102A

105

E102

FS104

101A

104 107

108

P104

MIX112

130B

C105

112

P101

137A

MIX141

141

136

FS133

133

135

134

P103

S104

S105

122

123

126

MIX128

125

127128

MIX142

142

124

V103

V104

FS121

V122

V123121B

121A

V102

Revankar-32

Revankar-33

Section II : H2SO4 decomposition

202C

203

204A 204B

205

206A 206B

207

208A 208B

209

210A

210B

211A

212

211B

220A

220B

220C

221

S3

Q

S2

S1

222 223 224 226227

218

216

S6

219

228

229

230A

230B

225

201B

S5Q

S4B

202B

231B

232A 232B

HE1 HE2 HE3 HE4 HE5 HE6 HE7 HE8 HE9 HE10 HE11

S4A

213A

214

215A

217A

227A227B

S4CQ

E202-F1

E202-F2E202-F3

E202-F4

S201

E210

P201

E205E203T

RECUP1DECOMP1 DECOMP2

RECUP2

C201

S205

P202DECOMP3DECOMP4

E201TUBE

P203

MIXER

E209S

HDECOMP4 HDECOMP3 HDECOMP2 HDECOMP1 HVAPORZR HPREVAPR HFLASH4 HFLASH3 HFLASH2 HPREHEAT

E201-1T

S202

S203

E203S

E202-2T E202-3T E202-4T

S204

E202-1SE201S E208

S7Q

Revankar-33

Revankar-34

Section II, Total Mixture

0

2

4

6

8

0 10 20 30 40 50

Stream No.

Mo

le F

low

, km

ol/

hr

Present Analysis

GA Analysis

Section II, O2

0

0.1

0.2

0.3

0.4

0.5

0.6

0 10 20 30 40 50

Stream No.

Mo

le F

low

, km

ol/

hr

Present Analysis

GA Analysis

Section II, H2SO4

0

0.5

1

1.5

2

0 10 20 30 40 50

Stream No.

Mo

le F

low

, km

ol/

hr

Present Analysis

GA Analysis

Section II, SO2

0.0

0.2

0.4

0.6

0.8

1.0

1.2

0 10 20 30 40 50

Stream No.

Mo

le F

low

, km

ol/

hr

Present Analysis

GA Analysis

Section II : H2SO4 decomposition

Revankar-34

Revankar-35

FEED

SIDELIQ

SIDEVAP

TOP

H2PROD

BOTTOM

COLUMN

SEP

E304

E305

Section III : HI decomposition

(HI, H2O, I2)

-Reactive distillation column -7stages -Feed : bubble temperature (300ºC) -Liquid draw

Revankar-35

Revankar-36

Simplified Chemical plant modeling

Revankar-36

Revankar-37

Catalytic H2SO4/SO3 decomposition

Rate limitation of H2SO4 decomp. is SO3

decomposition

Temperature, energetic limiting step of the SI cycle

Maximum temperature – safety margin for HTR

Extracted data (20+ papers) suggests Pt or Fe-oxides

Pt/Pd (~ No pressure depend.), oxides (P , activity

)

37 Brown 2011

MO + SO3 (MSO3) MO2 + SO2 , MO2 MO +O2

Revankar-38

Chemical plant models

S.S. flow rates & concentrations: ASPENPlus flowsheets

Chemical kinetics models for each reaction (literature)

Simplify or neglect reactant separation and concentration

processes, focus on the fundamental physics

38

SO2+I2+2H2O H2SO4 + 2HI

(Bunsen reaction, Kinetics rate constants: Brown 2003)

SO3 SO2 + ½ O2

(Sulfur trioxide decomp., rate const: Spewock 1976) 2HI I2 + H2

(Hydrogen iodide decomp., rate const: Laidler 1965/NIST) Enthalpies, reaction heat, heat of vaporization, and specific heat from: (NIST, ChE Handbook)

Revankar-38

Revankar-39

Chemical Plant Models

39

SO2+I2+2H2O H2SO4 + 2HI

(Bunsen reaction, Brown 2003)

SO3 SO2 + ½ O2 (Spewock 1976) 2HI I2 + H2 (,Laidler 1965)

Reverse reaction rate is non-negligible

Molar balance, energy balance for each species within the chemical plant

P, Tin

, mi,in

, hi,in

QHX

P, TR

, mi,out

, hi,out

Reaction Chamber

P, VR, M

R, T

R

yi(t), h

i

Assumptions Ideal gas mixture Negligible kinetic and potential energy No works, no heat loss Constant reactor volume Well mixed in the reaction chamber

Revankar-39

Revankar-40

Governing Equations in the Reaction Chamber

Species molar

balance

Global molar

balance

Energy balance

Chemical reaction

HX energy balance

Equation of state

,

i

R i in i in i

dy dX dXM y m m

dt dt dt

dt

dXmm

dt

dMoutin

R

dt

dPVQ

dt

dXhhhm

dt

dTcM RHXRXN

i

iiniiniR

PR )( ,,

iR CTXX ,

)( ,, outHeinHeHeHX hhmTAUQ

RRR RTMPV

(n+5) Equations vs. (n+6) Unknowns: MR, X, yi (i=1,2,,,n), mout, P, TR and THe,out

i=1,2,,,n

Recycling considered within each chemical plant section

H2O, I2, HI

Section 2 is essentially Plug flow reactor (PFR), section 1 and 3

Continuously stirred tank reactors ( CSTR)

Molar flow rate out of section 3 varies with reaction rate

Revankar-40

Revankar 41

Flowchart-Transient

Initiating

event &

time step

Steady State Parameters

P, TR, V

R, M

R, y

i , T

in, m

in, m

out

dX/dt, QHX

, THe,in

, THe,out

, U, A, mHe

Equation of

State

Reaction

Kinetics

Energy Balance

HX Energy

Balance

Global Molar

Balance

Species Molar

Balance y

i

dX/

dt

TR

MR&m

out

or

P&mout

or

MR&P

End

End of

Transient ?

Model Assumption

P=constant or

MR=constant or

mout

=constant

No

Yes

Thermo-

dynamic &

kinetic data

THe,out

Input values

Reaction

Chamber 1 2 3

Reactor

Volume, m3 6.79 1.66 57.32

HX Heat

Load, kJ N/A 417 46.6

HX

HTC*Area

(UA), W/K

N/A 2193 120

Helium Flow,

mol/s N/A 44.57 4.99

Revankar-41

Revankar-42

V & V: Chemical plant models

Chemical kinetics to data

from 20+ examples in bench

scale

ASPENPlus: benchmarked to

GA flowsheets

Reaction chamber model

valid. to SNL ILS H2SO4

decomp.

Entire SI loop validated to

available data from ILS at

JAERI and Tshingua

42

Rodriguez, et al. 2009

Brown 2011

Revankar-43

Modeling PBMR-268

THERMIX-Direkt is used to model the reactor thermal-

hydraulics

• THERMIX models the solid portions of the core via

mesh-averaging

• Direkt models the time dependent equations for

convective heat transfer and Helium flow in the core

• Includes models for decay heat

PARCS-THERMIX PBMR-268 benchmark model is used to

provide flux distributions in the core at steady state

Point kinetics model is used to solve for the reactor

behavior during transient

Point kinetic model used was benchmarked to PARCS-

THERMIX

Revankar-43

Revankar-44 44

PARCS: US NRC best

estimate code for

neutronics analysis

PARCS 3-D flux profileused as shape function

(Seker 2007)

Core flux profiles and point kinetic model

Revankar-44

Revankar-45

PBMR-268 - Steady state THERMIX-Direkt result

Revankar-46

Safety -Coupled HTR and Hydrogen

Production Facilities

Phenomena Identification and Ranking Table (PIRT)

1. Accidents at the chemical plant –Chemical release (H2,

O2, corrosive toxic, flammable, suffocating)

2. Process thermal events (loss of heat load, temperature

transients)

3. Failures of the intermediate heat-transport system (IHX ,

PHX failure, coolant or intermediate fluid loss )

4. Accidents in the nuclear plant (generic power or thermal

initiated transients, radiological release through coolant

leakage)

Revankar-46

Revankar-47

MELCOR

Power Conversion

Thermo-chemical

Hydrogen

Production Plant

H2 H2O O2

Intermediate

Heat Exchanger

GUI / End User

Models in Codes

SI Cycle

Implementation in

MELCOR code

(Sandia National Lab)

Revankar-48

Cost Comparison of Various H2 Generating

Technologies

0.68

1.691.83

1.38

1.12

1.76

1.98

5.64

0

1

2

3

4

5

6

Pro

duct

ion

Cos

t ($/

kg)

Coal

Gasification

Non-Catalytic

Partial

Oxidation

Solar Power Thermo

Chemical

Nuclear

Steam

Methane

Reformation

(Large Plant)

Steam

Methane

Reformation

(Small Plant)

Electrolysis

(Low

Estimate)

Electrolysis

(High

Estimate)

Production Method

Hydrogen Production Cost for Various Methods

Revankar-49

Hydrogen Storage Today

Compressed Fuel Storage Cylindrical tanks - most mature technology,

Liquified H2 Storage Cryotanks,

HP Liquid Tanks –

About one-third of the energy is lost in the process.

Solid State Conformable Storage Hydride material, Carbon Absorption

Chemical Hydrides Off-board Recycling

Revankar-50

Technologies for Hydrogen Storage

Revankar-51

Technology Need for Storage Improvements

Revankar-52

Catalyst Development for NaBH4 Hydrolysis

NaBH4 + 2H2O + Catalyst NaBO2 + 4H2 + HEAT

0

0.2

0.4

0.6

0.8

1

1.2

20 30 40 50 60 70 80

Degrees 2Theta

I/I_

ma

x

Co3B 400CXRD - Co3B

Ni, Cr, Ru

SEM -CoxB

Particle sizes range from 50-300nm

Revankar-53

E

A

C

B

1:34:23

D

A: Graduated Cylinder

B: Height Adjustable Outflow Line

C: Water Displacement Flask

D: Stop Watch

E: Reaction Chamber with Temperature Control

T = 60oC, P = 1 atm

Catalyst Development for NaBH4 Hydrolysis

CoxB on Ni Foam

(1cmx1cm)

Hydrogen production power equivalent per unit area for

10 wt% NaBH4 and 5 wt% NaOH at 60oC.

Hydrogen Production Power Equivalent Per Unit Area for 10 wt% NaBH4 and 5

wt% NaOH at 60 C.

Ni Foam

0.38

CoB

1.54

RuB

3.35

0

0.5

1

1.5

2

2.5

3

3.5

4

W/c

m^

2

A

B

C

D

E

F

G

A: Flexible Band Heater

B: Water Bath

C: ‘K’ Type Thermocouple

D: Stainless Steel Pressure Vessel

E: Reacting Solution

F: Pressure Release Valve

G: Pressure Transducer (0-2000psi)

A

B

C

D

E

F

G

A

B

C

D

E

F

G

A: Flexible Band Heater

B: Water Bath

C: ‘K’ Type Thermocouple

D: Stainless Steel Pressure Vessel

E: Reacting Solution

F: Pressure Release Valve

G: Pressure Transducer (0-2000psi)

Catalysis of NaBH4 at 0 psi Initial Pressure

180g H2O and 0.06g Ru at T = 60C

0

200

400

600

800

1000

1200

0 1000 2000 3000 4000 5000

Time (sec)

Pre

ssu

re (

psi)

Revankar-54

Hydrogen Delivery Technologies

• An economic strategy is required for the transition to a hydrogen delivery

system.

• Full life-cycle costing has not been applied to delivery alternatives.

• Hydrogen delivery technologies cost more than conventional fuel delivery.

• Current dispensing systems are inconvenient and expensive

Revankar-55

Delivered H2 Cost

Revankar-56

Hydrogen Conversion Technologies

Revankar-57

Revankar-58

PEM FC Research Challenges

Current density [A/cm2]

Cell

vo

ltag

e [V

]

•High catalytic activity

•Low gas permeability

•Low contact resistance

•High proton conductivity

Present

Target •Gas diffusion control

•Water management

eff

ecti

ven

ess

loss

loss

eff

ecti

ven

ess

Efficiency Improvements

Increase Range

Revankar-59

New materials and synthetic approaches • Electrolytes, anodes, cathodes

- Higher conductivity, chemical stability, improved mechanical properties, exploratory materials synthesis

- Ceramic proton conductors

- Improved electrokinetics, nanostructured architecture, functionally graded interfaces

• Interconnects with ‘metallic conductivity, ceramic stability’

• High strength, thermally shock resistant, chemically compatible materials for seals

Modeling ionic and electronic transport processes in bulk, at surfaces and across interfaces

New techniques for characterization of electrochemical processes

Innovative fuel cell architectures

Fuel Cells and Electrocatalysts : Emerging

technologies

Revankar-60

Future world energy demands, current fossil fuel limitations and environmental concerns -lead to alternate energy carrier. fuel media

Hydrogen seems most suitable fuel that meets the environmental, global, and geographical needs.

There are technological challenges and opportunities for immediate future and long term on developing infrastructure for hydrogen as an energy carrier

Technological advances are being made in hydrogen generation, storage, and conversion.

There is great potential in developing new technology to realize hydrogen economy.

Conclusions

Revankar-61

Jules Verne

(1828-1905)

The Mysterious

Island

PART 2 Chapter 11

" Yes, my friends, I believe that water will

one day be employed as fuel, that

hydrogen and oxygen which constitute it,

used singly or together, will furnish an

inexhaustible source of heat and light. .”

(1874)

Revankar-62

Questions ?