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HYDROGEN PRODUCTION FROM NATURAL GAS WITH VERY LOW CO2INTENSITY
Julian Straus, Vidar Skjervold,Rahul Anantharaman, David Berstad
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Overview
• Natural gas reforming – process description
• Recap: Improved process configuration
• CO2 liquefaction as separation technology
• Analysis of operation conditions
• Comparison to aMDEA + PSA process
• Conclusion
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Natural gas reforming
3
• Hydrogen separation technologies:• Pressure swing adsorption
(PSA)
• Palladium membrane(Pd)
• Focus on:• Recap of last results
Combustor
Pre-reformer
Water-gas shiftsection
Hydrogenseparation
Natural gasfeedstock
Shiftedsyngas
Auto-thermal reformer
O2
Tail gas tocombustor
CO2
Cryogenic air separation
Exhaust
O2 compression
Tail gasrecycle
Hydrogento liquefiers CO2
liquefaction
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Natural gas reforming
4
• Hydrogen separation technologies:• Pressure swing adsorption
(PSA)
• Palladium membrane(Pd)
• Focus on:• Recap of last results
• Improvements for CO2
liquefaction while maintaining similar CO2 capture rate
Combustor
Pre-reformer
Water-gas shiftsection
Hydrogenseparation
Natural gasfeedstock
Shiftedsyngas
Auto-thermal reformer
O2
Tail gas tocombustor
CO2
Cryogenic air separation
Exhaust
O2 compression
Tail gasrecycle
Hydrogento liquefiers CO2
liquefaction
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Recap: New process conditions
5
LT-LCO2 + Pd
LT-LCO2 + PSA
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CO2 liquefaction
• Process for simultaneous separation and liquefaction of CO2
• Costs of separation characterized by• Feed stream composition
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Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
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CO2 liquefaction
• Process for simultaneous separation and liquefaction of CO2
• Costs of separation characterized by• Feed stream composition
• Separation conditions (p and T)
7
Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
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CO2 liquefaction
• Process for simultaneous separation and liquefaction of CO2
• Costs of separation characterized by• Feed stream composition
• Separation conditions (p and T)
8
Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
• Heat integration
• Refrigeration cycle performance
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Impact of separation conditions
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Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
LT-LCO2 + Pd
LT-LCO2 + PSA
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Impact of separation conditions
10
Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
Pd membrane Pressure Swing Adsorption
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Refrigeration cycle performance
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Heat integrationCompression
From H2separation
Refrigeration cycle
CO2 separation
Compression
Liquid CO2
Tail gas
• Performance depending on distribution of cooling duties
• Different feed conditions result in different performance improvements
• Potential for further improvement through rigorous optimization
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Comparison to aMDEA-PSA technology
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84.7
78.0
83.6
50
90
80
70
60
Effic
ienc
y HH
V [%
]
96.1
92.7
96.4
80
95
90
85CO2
capt
ure
rate
[%]
9.3
17.4
8.7
0
15
10
5
CO2
inte
nsity
[g C
O2/
kWh L
HV]
*Without CO2
from power and upstream natural gas emissions
aMDEA + PSA
LT-LCO2 + Pd
LT-LCO2 + PSA
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Comparison to aMDEA-PSA technology
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aMDEA + PSA
LT-LCO2 + Pd
LT-LCO2 + PSA
89.1
100
89.9
85
95
90
Rela
tive
volu
met
ric fl
owra
te N
G [%
]
• Improved performance through:• Reduced natural gas demand
• Increased carbon capture ratio
• Novel process layout (to be published in a paper)
• Requires however more external power through lower power generation
14.4
-21.
8
21.6
-25
20
0-5
Net
pow
er d
eman
d [W
h/ k
Wh L
HV]
-10-15-20
1510
5
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Conclusion
• Natural gas reforming with carbon capture has potential for:• Very low CO2 intensity of hydrogen
• High efficiencies independently of the hydrogen separation technology
• Liquefaction of CO2 as separation technology:• Relatively new technology with further potential for improved performance above the
achieved 20 % reduction in energy consumption
• Based on widely applied unit operations
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Acknowledgements
This publication is based on results from the research project Hyper, performed under the ENERGIX programme. The authors acknowledge the following parties for financial support: Equinor, Shell, Kawasaki Heavy Industries, Linde Kryotechnik, Mitsubishi Corporation, Nel Hydrogen, Gassco and the Research Council of Norway (255107/E20).