Preliminary Techno-Economic Analysis of Hydrogen Carriers

Preliminary Techno-economic Analysis of Hydrogen Carriers Dr Ned Stetson Program Manager Hydrogen and Fuel Cell Technologies Office Hydrogen Technologies Program

HTAC Washington DC

March 9 2020

What are hydrogen carriers

bull Programrsquos definition

ndash Hydrogen carriers are hydrogen-rich liquid or solid phase materials from which hydrogen can be liberated on-demand Ideal hydrogen carriers have relatively high hydrogen densities at low pressure and near ambient temperature

bull Consensus from November workshop on hydrogen carriers

ndash Keep a broad definition of hydrogen carriers and let the requirements for specific applications narrow the scope of hydrogen carriers for consideration for those applications

2 US DEPARTMENT OF ENERGY OFFICE OF ENERGY EFFICIENCY amp RENEWABLE ENERGY FUEL CELL TECHNOLOGIES OFFICE

Examples of program activities on hydrogen carriers to date

bull Prior to 2010 ndash supported Air Products and Chemicals to investigate heterocyclic materials as potential hydrogen storage materials focused efforts on n-ethylcarbazole

bull 2018 ndash Initiated techno-economic analysis at Argonne National Lab to establish a baseline comparison between conventional compressed and liquid hydrogen delivery with several commonly cited hydrogen carriers

bull 2018 ndash Initiated preliminary efforts within HyMARC to investigate hydrogen carrier materials with an emphasis on ldquoadditionalrdquo potential benefits (eg chemical compression)

bull 2019 ndash included a topic in the FCTO FOA on hydrogen carriers selected 4 projects to investigate and develop novel hydrogen carrier concepts

bull Nov 2019 ndash Held a hydrogen carrier workshop in Golden CO - 74 participants representing industry universities and national labs and from N America Europe and Asia


For Techno-Economic Analysis (TEA) ndash where system boundary is set and the pathway followed matters

E N E R G Y T E C H N O LO G IE S AR E A E N ER G Y AN A L YS IS A N D E N VIR O N M EN T A L I MPA C T S D IVIS IO N

Compressor Cooling

system

HCOOH Dehydrogenation

HCOOH

Transportation

CO2

storage

CO2

hydrogenation

amp HCOOH

fueling

CO2

Transportation

HCOOH

storage Filling

station Direct

HCOOH

FCEV

FCEV

HCOOH Refueling Station

CO2

source

CO2 storage

amp

fueling

Compressor H2

source Compressor High-P

buffer

system

Cooling

system

Filling

station

High

Mid

Low

H2 Refueling Station (Baseline)

Compression Transportation

(Baseline)

H2 storage

amp fueling

H2 storage

amp fueling HCOOH

dehydrogenation

Path 1

Path 2

H2

Transportation

Energy amp

Other

Material

Flows

Emissions

Recycling amp

Disposal


Baseline TEA of hydrogen carriers with compressed hydrogen

bull All cases

ndash 50000 kg H2day delivery to city gate terminal

ndash Includes 10 days of storage at city gate terminal

bull Hydrogen Carriers

ndash Carriers transported from point of production to storage terminal

ndash Carriers transported 150 km from storage terminal to city gate terminal

ndash H2 release at city gate terminal

ndash Local distribution as compressed gaseous hydrogen to refueling stations

ndash Two-way carriers include transportation costs back to production site

bull Gaseous Hydrogen case

ndash H2 production using SMR

ndash Transmission as in trailer trucks for 150 km to city gate terminal

ndash Local distribution to hydrogen refueling stations 5 US DEPARTMENT OF ENERGY OFFICE OF ENERGY EFFICIENCY amp RENEWABLE ENERGY FUEL CELL TECHNOLOGIES OFFICE

Gaseous hydrogen baseline

$495kg H2 delivery to fueling station for gaseous hydrogen

50 tonne H2 per day by SMR 150 km from production site to terminal trailer truck transport transmission and distribution costs combined


Hydrogen carriers included in baseline study

bull One-way carriers

ndash Ammonia (separate H2 production step)

ndash Methanol (direct with no separate H2 production step)

bull Two-way carrier

ndash Methylcyclohexanetoluene MP BPoC

oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst

Non-PGM Catalyst PtAl2O3 Catalyst

High-Temperature Cracking

Ni Catalyst

Steam Reforming

Production DecompositionH2 Capacity

Haber-Bosch Process

Fe Based Catalyst


Factors to consider for hydrogen carriers

1 Capacity of carrier productiondehydrogenation plants

a Production - assumed plants not built and sized just based on targeted H2 delivery per day

b Dehydrogenation - plants are sized for targeted hydrogen capacity

2 Production - cost and energy to produce hydrogenated carrier

3 Transmission ndash cost to delivery carrier from point of production to storage terminal (rail ship pipeline etc) and then to city gate (150 km by truck)

a For two-way carriers - includes cost to return dehydrogenated product to hydrogenation site

4 Dehydrogenation - cost and energy to dehydrogenate and release the hydrogen from the carrier at the city gate terminal

a Includes purification costs to clean-up the hydrogen

b For two-way carriers ndash includes replacement costs of lost carrier (eg evaporation side reactions etc)

Production Transmission Dehydrogenation Distribution 8 US DEPARTMENT OF ENERGY OFFICE OF ENERGY EFFICIENCY amp RENEWABLE ENERGY FUEL CELL TECHNOLOGIES OFFICE

Plant capacity matters

Example ndash methanol ndash production method can change as plant capacity varies to reduce capital costs


Levelized cost for production

bull Levelized production cost for methanol the lowest when produced in high capacity plants (10k tonday)

bull Methylcyclohexane production through hydrogenation of toluene competitive with methanol levelized production cost

bull Ammonia production highest on a levelized production cost plants more capital intensive than methanol plants


Transmission from point of production to city gate

Production Transmission Dehydrogenation Distribution

NG

Water

MeOH

Methanol Production

Methanol Decomposition

MeOH

Utilities

H2

H2 Purification ndash ISOSAE

H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal

Liquid Methanol CarrierLarge Plant

Electricity

Storage amp Transportation Infrastructure

Storage Terminal

Transmission

Central Production Plant

City Gate

3000-5000 tpd

bull Large-scale methanol and ammonia production planes with low-cost natural gas located in gulf coast region

bull H2 refueling stations are located in California

H2

station locations

3250 km

150 km


Transmission cost comparison through various means

bull H2 capacity of the carrier is an important factor in determining the transmission cost by rail - Toluene has nearly the same train transmission cost as methanol on tpd basis but is gt3X costlier on kg-H2

basis

bull Toxicity and handling are also important factors in determining rail transmission costs - Ammonia has nearly the same H2 capacity as methanol but is gt2X costlier to move by train

bull Long H2 or carrier pipelines (gt1000 mile) do not offer significant cost savings - Pipelines may not be economically viable for two-way carriers

Comparison costs by rail by pipeline by ship for MCHtoluene

Railroad Waybill 2016 Data

$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD


Levelized transmission cost comparison

Methanol transmission lowest methylcyclohexane more costly due to return leg

bull Unit train (once every 10 days) to storage terminal in California (3250 km)

bull Local transmission by truck (150 km) to city gate terminal

bull Similar case for both methanol and ammonia methylcyclohexane includes return leg for toluene


Capital cost of methylcyclohexane dehydrogenation plant


MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC

H2 Purification amp Condensation

Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols

High grade waste heat

20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10

Heat 036 kWhthkWhth -H2

FeedstockUtilities

NG 022 kWhthKWhth -H2

Electricity 004 kWheKWth -H2

Capital Cost Factors 50 tpd-H2

Dependence of capital costs on capacity


Levelized decomposition cost comparison

Levelized decomposition costs (LDC) are

comparable for the three carriers 061-078

$kg-H2 at 50 tpd-H2

At high throughput LDC decreases most for

ammonia However ammonia decomposes at

a high temperature (800oC) using a catalyst

(Ni) that may require further development and

field testing

Methanol decomposition method well

established but requires steam reforming and

water gas shift catalysts Cost may decrease if

methanol reformed at gt3 atm

MCH decomposes at 2 bar using a PGM

catalyst (PtAl2O3) and requires a large

compressor


Distribution costs

TRANSPORTATION

City-Gate Terminal to Refueling Comparing distribution as 350 amp 500 bar Station ldquoLast-Milerdquo Distribution compressed H2 and liquid H2 for various

distances

Some key initial findings bull Cost savings for cH2 do not scale at higher pressures bull The number of cH2 trucks required increases rapidly

with distance bull LH2 costs dominated by liquefaction cost and energy

penalty (32)

For baseline analysis all cases kept constant bull 400 kg H2day dispensing rate at fueling station bull Trailer capacity of 1024 kg 36 m3 volume


Baseline levelized cost of H2 at 50000 kg per day

bull At 50000 kg H2 per day methanol produced at high volume in the gulf coast area and transport to California can be cost competitive with ldquolocallyrdquo produced gaseous hydrogen

bull Ammonia and methylcyclohexane have a cost premium over ldquolocallyrdquo produced gaseous hydrogen FUEL CELL TECHNOLOGIES OFFICE US DEPARTMENT OF ENERGY OFFICE OF ENERGY EFFICIENCY amp RENEWABLE ENERGY 17

Levelized costs of H2 at various daily demands


Storage capacity defined as the g H l of material

Analysis of formate salts as hydrogen carriers

Electrochemistry enables regeneration of H2

carrier lsquowithout hydrogenrsquo

∆Go = 0

2

Volumetric capacity

Preliminary TEA suggests water removal is the most expensive process

TEA analysis suggests efforts are needed to perform regeneration at higher concentrations or a use case with cheap source of heat eg nuclear reactor

Deliverable capacity limited by the solubility of formate at 20 degC Usable capacity limited by the solubility of bicarbonate at 60 degC


Summary

bull Hydrogen carriers can be cost competitive with gaseous hydrogen production

ndash Production capacity can influence cost competitiveness

ndash Transmission costs can vary depending on nature of the hydrogen carrier

ndash Two-way carriers are disadvantaged by two-way transportation costs and replacement costs

bull Application specific requirements need to be considered when determining suitability of a hydrogen carrier

bull Boundary conditions should be considered when comparing different TEAs

bull Future activities

ndash Including comparison with liquid hydrogen transmission and distribution

ndash Expand analysis of other types of hydrogen carriers (eg formate salts)

ndash Investigation of impact of yield cycle life energy use etc

ndash Consider other potential benefits (eg chemical compression)


Acknowledgements

bull Argonne National Laboratory

ndash Rajesh Ahluwalia

ndash DD Papadias

ndash J-K Peng

bull Lawrence Berkeley National Laboratory

ndash Hanna Breunig

ndash Aikaterini Anastasopoulou

bull Pacific Northwest National Laboratory

ndash Tom Autrey

ndash Kat Grubel

ndash Kriston Brooks


Thank you for your attention

Dr Ned Stetson Program Manager ndash Hydrogen Technologies

Hydrogen amp Fuel Cell Technologies Office NedStetsoneedoegov


wwwhydrogenenergygov

What are hydrogen carriers

bull Programrsquos definition

ndash Hydrogen carriers are hydrogen-rich liquid or solid phase materials from which hydrogen can be liberated on-demand Ideal hydrogen carriers have relatively high hydrogen densities at low pressure and near ambient temperature

bull Consensus from November workshop on hydrogen carriers

ndash Keep a broad definition of hydrogen carriers and let the requirements for specific applications narrow the scope of hydrogen carriers for consideration for those applications











Compressor Cooling

system


HCOOH

Transportation

CO2

storage

CO2

hydrogenation

amp HCOOH

fueling

CO2

Transportation

HCOOH

storage Filling

station Direct

HCOOH

FCEV

FCEV


CO2

source

CO2 storage

amp

fueling

Compressor H2


buffer

system

Cooling

system

Filling

station

High

Mid

Low



(Baseline)

H2 storage

amp fueling

H2 storage

amp fueling HCOOH

dehydrogenation

Path 1

Path 2

H2

Transportation

Energy amp

Other

Material

Flows

Emissions

Recycling amp

Disposal



bull All cases























oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel

















Compressor Cooling

system


HCOOH

Transportation

CO2

storage

CO2

hydrogenation

amp HCOOH

fueling

CO2

Transportation

HCOOH

storage Filling

station Direct

HCOOH

FCEV

FCEV


CO2

source

CO2 storage

amp

fueling

Compressor H2


buffer

system

Cooling

system

Filling

station

High

Mid

Low



(Baseline)

H2 storage

amp fueling

H2 storage

amp fueling HCOOH

dehydrogenation

Path 1

Path 2

H2

Transportation

Energy amp

Other

Material

Flows

Emissions

Recycling amp

Disposal



bull All cases























oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel










Compressor Cooling

system


HCOOH

Transportation

CO2

storage

CO2

hydrogenation

amp HCOOH

fueling

CO2

Transportation

HCOOH

storage Filling

station Direct

HCOOH

FCEV

FCEV


CO2

source

CO2 storage

amp

fueling

Compressor H2


buffer

system

Cooling

system

Filling

station

High

Mid

Low



(Baseline)

H2 storage

amp fueling

H2 storage

amp fueling HCOOH

dehydrogenation

Path 1

Path 2

H2

Transportation

Energy amp

Other

Material

Flows

Emissions

Recycling amp

Disposal



bull All cases























oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel









bull All cases























oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel


















oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel














oC wt gL P bar T

oC P bar T

oC DH

kJmol-H2

Ammonia

-78 -334 176 121 150 375 20 800 306

Methanol

-98 647 1875 149 51 250 3 290 166

MCH

-127 101 61 47 10 240 2 350 683

CuZnOAl2O3 Catalyst



Ni Catalyst

Steam Reforming


Haber-Bosch Process

Fe Based Catalyst























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel





























NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel


















NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel















NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel










NG

Water

MeOH

Methanol Production


MeOH

Utilities

H2


H2NG

+ CO CO2MeOH

Transmission

StorageGH2 Terminal


Electricity


Storage Terminal

Transmission


City Gate

3000-5000 tpd



H2

station locations

3250 km

150 km




basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel










basis





$111

$158 147

$035

$024

015$146

$182

162

$00

$05

$10

$15

$20

$25

$30

1 Ship 2 Ships Rail

$k

g-H

2

Transmission

Port Facilities

$070$098

147$023

$015

01

$093

$112

$157

1 Ship 2 Ships Rail

$051

$098

147$018

$015

005

$070

$112

$152

1 Ship 2 Ships Rail

$055

$147018

$004

$073

$151

3 Ships Rail

50 TPD 130 TPD










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel
















MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel










MCH Tank

TOL (~100)

Toluene Tank H

2M

CHT

OL

C7H

14(g

)

350 degC

PSA

To Burner

H2 ISOSAE Standard

Tailgas (13 atm)

MCH (~100)

255 degC256 kWth

4 stagesIntercooled

40 degC1

5 a

tm

40 degC


Compression

2 at

m

Dehydrogenation

20 atm

Storage 1

PSA Tailgas

NG 012 mols


20

8a

tm

Storage 2

Are

a 200

Area 101

Area 102

Area 300

Area 400

C7H

14(l

)

System Boundary

70 deg

C2

50

degC

C7H

8(l

)

Chill

er

To Storage

Losses

Toluene+MCH 084

Hydrogen 10


FeedstockUtilities









$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel











$kg-H2 at 50 tpd-H2





field testing







compressor


Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel








Distribution costs

TRANSPORTATION


distances



penalty (32)












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel

















∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel














∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel












∆Go = 0

2

Volumetric capacity





Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel








Summary













Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel








Acknowledgements



ndash DD Papadias

ndash J-K Peng


ndash Hanna Breunig



ndash Tom Autrey

ndash Kat Grubel













Documents

Preliminary Techno-Economic Analysis of Hydrogen Carriers