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Frontiers in Energy

ISSN 2095-1701

ISSN 2095-1698(Online)

CN 11-6017/TK

邮发代号 80-972

2019 Impact Factor: 2.657

Frontiers in Energy  2023, Vol. 17 Issue (5): 585-610   https://doi.org/10.1007/s11708-023-0886-4
  本期目录
Production of hydrogen from fossil fuel: A review
Shams ANWAR, Xianguo LI()
Laboratory for Fuel Cell and Green Energy, Department of Mechanical and Mechatronics Engineering, University of Waterloo, Waterloo, Ontario N2L3G1, Canada
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Abstract

Production of hydrogen, one of the most promising alternative clean fuels, through catalytic conversion from fossil fuel is the most technically and economically feasible technology. Catalytic conversion of natural gas into hydrogen and carbon is thermodynamically favorable under atmospheric conditions. However, using noble metals as a catalyst is costly for hydrogen production, thus mandating non-noble metal-based catalysts such as Ni, Co, and Cu-based alloys. This paper reviews the various hydrogen production methods from fossil fuels through pyrolysis, partial oxidation, autothermal, and steam reforming, emphasizing the catalytic production of hydrogen via steam reforming of methane. The multicomponent catalysts composed of several non-noble materials have been summarized. Of the Ni, Co, and Cu-based catalysts investigated in the literature, Ni/Al2O3 catalyst is the most economical and performs best because it suppresses the coke formation on the catalyst. To avoid carbon emission, this method of hydrogen production from methane should be integrated with carbon capture, utilization, and storage (CCUS). Carbon capture can be accomplished by absorption, adsorption, and membrane separation processes. The remaining challenges, prospects, and future research and development directions are described.

Key wordsmethane    catalytic conversion    natural gas    hydrogen production    CCUS
收稿日期: 2023-03-22      出版日期: 2023-11-09
Corresponding Author(s): Xianguo LI   
 引用本文:   
. [J]. Frontiers in Energy, 2023, 17(5): 585-610.
Shams ANWAR, Xianguo LI. Production of hydrogen from fossil fuel: A review. Front. Energy, 2023, 17(5): 585-610.
 链接本文:  
https://academic.hep.com.cn/fie/CN/10.1007/s11708-023-0886-4
https://academic.hep.com.cn/fie/CN/Y2023/V17/I5/585
Fig.1  
Methods and sources of hydrogen productionAdvantageDisadvantageTemperature range/°CEnergy efficiency/%Hydrogen production cost/($·kg?1)Refs.
SRM (liquid fuel and natural gas)Conventional technology and developed infrastructureFormation of CO and CO2 as the by-products700–100074–852.27[4,17,21,22,3137]
Gasification of solid fuel (coal)Feedstock is cheap and available in large quantities in nature; the process has no CO2 emissionHydrogen production is inconsistent due to feedstock containment, heavy oil generation, and tar formation700–100060–751.48[4,17,21,22,3137]
Biomass processCost-effective and renewableCH4 as a by-product of hydrogen production, feedstock supply may vary800–100035–501.8–2.05[4,17,21,22,3137]
Water electrolysisNo carbon emission, valuable oxygen as a by-productChallenging storage and transport, safety concern50–100060–8010.30[4,17,21,22,3137]
Tab.1  
MethodsSources of feedMaximal conversion conditionOperating catalystsH2 yieldConversion efficiencyRef.
Hydrocarbon pyrolysisMethaneT = 1175 °C, P = 1 atm,Quartz bubble column using gallium78%91%[40]
t = 0.5 s for the bubbles
EthaneT = 200 °C, P = 0.1 MPa,Metal oxides and argon dilution70%80%[41]
Argon dilution of 93 mol.%
PropaneT > 950 °C,Molten mixture of 73∶27 mol.% of Bi and Ni in bubble column reactor60%100%[42]
t = 1 s in reaction
Partial oxidationMethaneT = 650 °C,Wet impregnation method using Ni-Al-H-600, or 10 wt.% Ni supported Al2O3 and Zr catalyst72%90%[43]
Catalyst time on stream = 7 h, at alumina and zirconia surface
MethanolT = 500 °C, t = 20 minUltra-low Pt and Pd contents and Al2O391.3%90%[44]
MethanolT = 350 °C,Iron chromium catalyst95%85%[45]
Pressure ratio of 0.015–0.05, N2O utilized in fluidized bed
Autothermal reformingMethaneT = 850 °C, P = 1 atm10 wt.% Ni–0.9 wt.% Re/Ce0.5/Zr0.5/Al2O383%85%[46]
Crude glycerolT = 550 °C,5 wt.% Ni catalyst70%100%[47]
S/C ratio (molar ratio of steam to carbon) = 2.6,
O2/C ratio (molar ratio of O2 to carbon) = 0.5,
t > 2 h
EthanolT = 600 °C, P = 1 atm10 wt.% Ni–0.4 wt.% Re catalyst65%100%[48]
Steam reformingMethaneT = 850 °C,10 wt.% Ni supported on SiC modified CAx/Al2O3 (NASC)75%81%[49]
t = 20 h to avoid coke formation on catalyst
GlycerolT = 650 °C, P = 1 atm,Unreduced 20% nickel55%80%[50]
in quartz microreactor
MethanolT = 300 °C, P = 0.1 MPa,Pd-Zn alloy-based catalyst86.3%98%[51]
Water/glycerol ratio (molar ratio of water to glycerol) = 1.2∶1,
t = 2 h
Tab.2  
Fig.2  
Fig.3  
MetalsSymbolsMelting point/°CBoiling point/°CDensity/(g·cm?3)Specific heat/(J·g?1·°C?1)Cost/($·kg?1)
NickelNi145527308.910.5023.78
CobaltCo149529008.900.4234.93
CopperCu108525628.960.384.96
MolybdenumMo2610556010.20.2594.72
Tab.3  
Fig.4  
Fig.5  
Fig.6  
CatalystsMetal loading/wt.%Temperature/°CCH4 conversion/%S/C ratioRef.
Ni/α-Al2O32.95004[112]
Ni-Al2O313800752.7[113]
Ni-Al2O3 honeycomb20.260079.12[114]
Ni/γ-Al2O312750952[115]
Ni0.4Mg0.6O750~1000.5[104]
Ni/MgO750903[116]
Ni/MgO-Al2O312.56503[105]
Ni/Mg-Al2O415.3650505[117]
Ni/Al2O4-Al2O317600803[118]
Ni/SiO210750~400.5[119]
Ni/TiO210450453[120]
Ni/Ce0.8Zr0.2O21555059.51[110]
Ni/SiO2/Al2O310650963.5[121]
Ni/La2/Sn2O712750302[122]
Ni/Y2/Zr2O710750942[123]
Ni/Y2/Ti2O77750~962[124]
Ni/LaTiO515.5900951[78]
NiLaO36.2650401.24[125]
Ni/LaFeO312800802[126]
Ni/La2O3-ZrO21065041.23[127]
Cu/Co6Al25700963[128]
Co-Pt-Zr-La/Al2O3570099.31.25[129]
Tab.4  
Fig.7  
Fig.8  
Fig.9  
Fig.10  
Fig.11  
Fig.12  
Fig.13  
Fig.14  
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