Hydrogen production from methanol partial oxidation over Pt/Al2O3 catalyst with low Pt content

Chen, Wei‐Hsin; Shen, Chun; Lin, Bo; Liu, Shih Chun

doi:10.1016/j.energy.2015.05.055

Cited by 56 publications

(18 citation statements)

References 33 publications

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“…Maps of Ti and Pd reflected the outline of chosen region. It illustrated that not only the support but also the active components distributed well [48]. Owing to the too scattered distribution of Pt, the map of it did not show any inerratic shape.…”

Section: Sem and Edsmentioning

confidence: 86%

Methanol total oxidation as model reaction for the effects of different Pd content on Pd-Pt/CeO2-Al2O3-TiO2 catalysts

Guo

Zhang

et al. 2017

Molecular Catalysis

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Section: Sem and Edsmentioning

confidence: 86%

Methanol total oxidation as model reaction for the effects of different Pd content on Pd-Pt/CeO2-Al2O3-TiO2 catalysts

Guo

Zhang

et al. 2017

Molecular Catalysis

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“…Eq. (1) indicates the reaction process for methanol catalytic combustion reaction [16][17][18][19] . The heating cartridges and A-type thermocouple on the inlet evaporation chamber plate for combustion and thermostat were used to perform the preheat of the microreactor before the heat-supply by the methanol catalytic combustion reaction for the microreactor itself.…”

Section: Structural Design Of Methanol Catalytic Combustion Microreactormentioning

confidence: 99%

Structural design of self-thermal methanol steam reforming microreactor with porous combustion reaction support for hydrogen production

Zheng

Zhou

et al. 2020

International Journal of Hydrogen Energy

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To replace the traditional electric heating mode and increase methanol steam reforming reaction performance in hydrogen production, methanol catalytic combustion was proposed as heat-supply mode of methanol steam reforming microreactor. Moreover, the methanol catalytic combustion microreactor and self-thermal methanol steam reforming microreactor for hydrogen production were developed. Furthermore, catalytic combustion reaction supports with different structures were designed. It was found that the developed self-thermal methanol steam reforming microreactor had better reaction performance. Compared with A-type, the △Tmax of C-type porous reaction support was decreased by 24.4℃ under 1.3 mL/min methanol injection rate. Moreover, methanol conversation and H2 flow rate of the self-thermal methanol steam reforming microreactor with C-type porous reaction support were increased by 15.2% under 10 mL/h methanol-water mixture injection rate and 340 ℃ self-thermal temperature. Meanwhile, the CO selectivity was decreased by 4.1%. This work provides a new structural design of the self-thermal methanol steam reforming microreactor for hydrogen production for the fuel cell.

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“…After CH 4 , methanol is the second most abundant organic compound in the atmosphere [28]. The process of catalytic oxidation of methanol enjoys great interest, mainly due to the possibility of hydrogen generation [29][30][31][32][33]. The necessity of rapid removal of heat generated in this process is the premise for carrying it out in a fluidised bed.…”

Section: Nitrous Oxide As a Greenhouse Gas And An Oxidantmentioning

confidence: 99%

Catalytic oxidation of methanol in the cenospheric fluidized bed

et al. 2019

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Original scientific paper https://doi.org/10.2298/TSCI19S4231BThe process of oxidation of gaseous CH 3 OH by N 2 O was carried out over an Ag-Fe 2 O 3 -cenosphere catalyst whose structure can be defined as double shell-core catalyst. Preparation of the catalyst was carried out in two stages: thermal decomposition of Fe(CO) 5 at above 160 °C and then electroless Ag plating. The process of methanol degradation by N 2 O was carried out in a fluidized bed reactor. The study confirms that it is possible to achieve complete degradation of N 2 O and CH 3 OH for the obtained catalyst at above 450 °C when the contact time of the reactants with the catalyst is approximately 6 second and when the substrates are used in stoichiometric ratios. More than 60% of the hydrogen contained in CH 3 OH can be converted to molecular hydrogen at 500 °C with a ratio of N 2 O/CH 3 OH not greater than 0.6 and with a contact time of reactants with the catalyst of approx. 6 seconds.

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Hydrogen production from methanol partial oxidation over Pt/Al2O3 catalyst with low Pt content

Cited by 56 publications

References 33 publications

Methanol total oxidation as model reaction for the effects of different Pd content on Pd-Pt/CeO2-Al2O3-TiO2 catalysts

Methanol total oxidation as model reaction for the effects of different Pd content on Pd-Pt/CeO2-Al2O3-TiO2 catalysts

Structural design of self-thermal methanol steam reforming microreactor with porous combustion reaction support for hydrogen production

Catalytic oxidation of methanol in the cenospheric fluidized bed

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