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Currently at Universidad Pública de Navarra,
PUBLICATIONS
2013
Bimbela, Fernando; Oliva, Miriam; Ruiz, Joaquín; García, Lucía; Arauzo, Jesús
Hydrogen production via catalytic steam reforming of the aqueous fraction of bio-oil using nickel-based coprecipitated catalysts Journal Article
In: International Journal of Hydrogen Energy, vol. 38, no. 34, pp. 14476–14487, 2013, ISSN: 03603199.
@article{Bimbela2013,
title = {Hydrogen production via catalytic steam reforming of the aqueous fraction of bio-oil using nickel-based coprecipitated catalysts},
author = {Fernando Bimbela and Miriam Oliva and Joaquín Ruiz and Lucía García and Jesús Arauzo},
url = {http://www.sciencedirect.com/science/article/pii/S0360319913022295},
issn = {03603199},
year = {2013},
date = {2013-11-01},
journal = {International Journal of Hydrogen Energy},
volume = {38},
number = {34},
pages = {14476--14487},
abstract = {Hydrogen production was studied in the catalytic steam reforming of a synthetic and a real aqueous fraction of bio-oil. Ni/Al coprecipitated catalysts with varying nickel content (23, 28 and 33 relative atomic %) were prepared by an increasing pH technique and tested during 2 h under different experimental conditions in a small bench scale fixed bed setup. The 28% Ni catalyst yielded a more stable performance over time (steam-to-carbon molar ratio, S/C = 5.58) at 650 °C and a catalyst weight/organic flow rate (W/morg) ratio of 1.7 g catalyst min/g organic. Using the synthetic aqueous fraction as feed, almost complete overall carbon conversion to gas and hydrogen yields close to equilibrium could be obtained with the 28% Ni catalyst throughout. Up to 63% of overall carbon conversion to gas and an overall hydrogen yield of 0.09 g/g organic could be achieved when using the real aqueous fraction of bio-oil, but the catalyst performance showed a decay with time after 20 min of reaction due to severe coke deposition. Increasing the W/morg ratio up to 5 g catalyst min/g organic yielded a more stable catalyst performance throughout, but overall carbon conversion to gas did not surpass 83% and the overall hydrogen yield was only ca. 77% of the thermodynamic equilibrium. Increasing reaction temperatures (600–800 °C) up to 750 °C enhanced the overall carbon conversion to gas and the overall yield to hydrogen. However, at 800 °C the catalyst performance was slightly worse, as a result of an increase in thermal cracking reactions leading to an increased formation of carbon deposits.},
keywords = {},
pubstate = {published},
tppubtype = {article}
}
Hydrogen production was studied in the catalytic steam reforming of a synthetic and a real aqueous fraction of bio-oil. Ni/Al coprecipitated catalysts with varying nickel content (23, 28 and 33 relative atomic %) were prepared by an increasing pH technique and tested during 2 h under different experimental conditions in a small bench scale fixed bed setup. The 28% Ni catalyst yielded a more stable performance over time (steam-to-carbon molar ratio, S/C = 5.58) at 650 °C and a catalyst weight/organic flow rate (W/morg) ratio of 1.7 g catalyst min/g organic. Using the synthetic aqueous fraction as feed, almost complete overall carbon conversion to gas and hydrogen yields close to equilibrium could be obtained with the 28% Ni catalyst throughout. Up to 63% of overall carbon conversion to gas and an overall hydrogen yield of 0.09 g/g organic could be achieved when using the real aqueous fraction of bio-oil, but the catalyst performance showed a decay with time after 20 min of reaction due to severe coke deposition. Increasing the W/morg ratio up to 5 g catalyst min/g organic yielded a more stable catalyst performance throughout, but overall carbon conversion to gas did not surpass 83% and the overall hydrogen yield was only ca. 77% of the thermodynamic equilibrium. Increasing reaction temperatures (600–800 °C) up to 750 °C enhanced the overall carbon conversion to gas and the overall yield to hydrogen. However, at 800 °C the catalyst performance was slightly worse, as a result of an increase in thermal cracking reactions leading to an increased formation of carbon deposits.
García, Gorka; Monzón, Antonio; Bimbela, Fernando; Sánchez, José Luis; Ábrego, Javier
Desulfurization and Catalytic Gas Cleaning in Fluidized-Bed Co-gasification of Sewage Sludge–Coal Blends Journal Article
In: Energy & Fuels, vol. 27, no. 5, pp. 2846–2856, 2013, ISSN: 0887-0624.
@article{Garcia2013c,
title = {Desulfurization and Catalytic Gas Cleaning in Fluidized-Bed Co-gasification of Sewage Sludge–Coal Blends},
author = {Gorka García and Antonio Monzón and Fernando Bimbela and José Luis Sánchez and Javier Ábrego},
url = {http://dx.doi.org/10.1021/ef400259g},
issn = {0887-0624},
year = {2013},
date = {2013-05-01},
journal = {Energy & Fuels},
volume = {27},
number = {5},
pages = {2846--2856},
publisher = {American Chemical Society},
abstract = {Energy recovery from digested sewage sludge can be achieved by means of co-gasification with coal in a fluidized-bed system. In this regard, one of the main hurdles in developing a feasible process is the need for gas cleaning, with special emphasis on desulfurization and minimization of the tar content of the product gas. In this work, high-temperature catalytic gas cleaning was investigated by means of two fixed beds placed in series downstream of the gasification system: the first containing dolomite for desulfurization and primary tar cracking and the second containing a nickel-based catalyst for additional gas reforming. The effect of the temperature on the performance of the Ni catalyst bed (800?900 °C) was assessed. The use of dolomite in a secondary bed at 800 °C allowed for a significant reduction in both tar [15?0.21 g/m3 standard temperature and pressure (STP)] and H2S (to less than 0.01%) and an increase in the heating value of the gas [lower heating value (LHV) from 2000 to 2800 kJ/m3 STP]. The use of the Ni catalyst decreased the tar content of the gas to undetectable levels. The best results were obtained with the Ni-based catalyst at 800 °C, in terms of enhanced LHV (increasing from 2000 to 3300 kJ/m3 STP), gas production, which increased from around 2.40 to 2.75 m3 STP/kg on a dry and ash-free basis (daf), and energy requirements for the process. However, some evidence of Ni catalyst deactivation was found when operating under these conditions. Energy recovery from digested sewage sludge can be achieved by means of co-gasification with coal in a fluidized-bed system. In this regard, one of the main hurdles in developing a feasible process is the need for gas cleaning, with special emphasis on desulfurization and minimization of the tar content of the product gas. In this work, high-temperature catalytic gas cleaning was investigated by means of two fixed beds placed in series downstream of the gasification system: the first containing dolomite for desulfurization and primary tar cracking and the second containing a nickel-based catalyst for additional gas reforming. The effect of the temperature on the performance of the Ni catalyst bed (800?900 °C) was assessed. The use of dolomite in a secondary bed at 800 °C allowed for a significant reduction in both tar [15?0.21 g/m3 standard temperature and pressure (STP)] and H2S (to less than 0.01%) and an increase in the heating value of the gas [lower heating value (LHV) from 2000 to 2800 kJ/m3 STP]. The use of the Ni catalyst decreased the tar content of the gas to undetectable levels. The best results were obtained with the Ni-based catalyst at 800 °C, in terms of enhanced LHV (increasing from 2000 to 3300 kJ/m3 STP), gas production, which increased from around 2.40 to 2.75 m3 STP/kg on a dry and ash-free basis (daf), and energy requirements for the process. However, some evidence of Ni catalyst deactivation was found when operating under these conditions.},
keywords = {},
pubstate = {published},
tppubtype = {article}
}
Energy recovery from digested sewage sludge can be achieved by means of co-gasification with coal in a fluidized-bed system. In this regard, one of the main hurdles in developing a feasible process is the need for gas cleaning, with special emphasis on desulfurization and minimization of the tar content of the product gas. In this work, high-temperature catalytic gas cleaning was investigated by means of two fixed beds placed in series downstream of the gasification system: the first containing dolomite for desulfurization and primary tar cracking and the second containing a nickel-based catalyst for additional gas reforming. The effect of the temperature on the performance of the Ni catalyst bed (800?900 °C) was assessed. The use of dolomite in a secondary bed at 800 °C allowed for a significant reduction in both tar [15?0.21 g/m3 standard temperature and pressure (STP)] and H2S (to less than 0.01%) and an increase in the heating value of the gas [lower heating value (LHV) from 2000 to 2800 kJ/m3 STP]. The use of the Ni catalyst decreased the tar content of the gas to undetectable levels. The best results were obtained with the Ni-based catalyst at 800 °C, in terms of enhanced LHV (increasing from 2000 to 3300 kJ/m3 STP), gas production, which increased from around 2.40 to 2.75 m3 STP/kg on a dry and ash-free basis (daf), and energy requirements for the process. However, some evidence of Ni catalyst deactivation was found when operating under these conditions. Energy recovery from digested sewage sludge can be achieved by means of co-gasification with coal in a fluidized-bed system. In this regard, one of the main hurdles in developing a feasible process is the need for gas cleaning, with special emphasis on desulfurization and minimization of the tar content of the product gas. In this work, high-temperature catalytic gas cleaning was investigated by means of two fixed beds placed in series downstream of the gasification system: the first containing dolomite for desulfurization and primary tar cracking and the second containing a nickel-based catalyst for additional gas reforming. The effect of the temperature on the performance of the Ni catalyst bed (800?900 °C) was assessed. The use of dolomite in a secondary bed at 800 °C allowed for a significant reduction in both tar [15?0.21 g/m3 standard temperature and pressure (STP)] and H2S (to less than 0.01%) and an increase in the heating value of the gas [lower heating value (LHV) from 2000 to 2800 kJ/m3 STP]. The use of the Ni catalyst decreased the tar content of the gas to undetectable levels. The best results were obtained with the Ni-based catalyst at 800 °C, in terms of enhanced LHV (increasing from 2000 to 3300 kJ/m3 STP), gas production, which increased from around 2.40 to 2.75 m3 STP/kg on a dry and ash-free basis (daf), and energy requirements for the process. However, some evidence of Ni catalyst deactivation was found when operating under these conditions.
Remón, Javier; Medrano, José A; Bimbela, Fernando; García, Lucía; Arauzo, Jesús
Ni/Al–Mg–O solids modified with Co or Cu for the catalytic steam reforming of bio-oil Journal Article
In: Applied Catalysis B: Environmental, vol. 132-133, pp. 433–444, 2013, ISSN: 09263373.
@article{Remon2013,
title = {Ni/Al–Mg–O solids modified with Co or Cu for the catalytic steam reforming of bio-oil},
author = {Javier Remón and José A Medrano and Fernando Bimbela and Lucía García and Jesús Arauzo},
url = {http://www.sciencedirect.com/science/article/pii/S0926337312005838},
issn = {09263373},
year = {2013},
date = {2013-03-01},
journal = {Applied Catalysis B: Environmental},
volume = {132-133},
pages = {433--444},
abstract = {An environmentally friendly method of producing a hydrogen rich gas is the catalytic steam reforming of bio-oil. This requires the development of a catalyst appropriate for the process. In the present work, five different research catalysts have been prepared and tested. A Ni/AlMg catalyst was selected as a reference. Modifications to the catalyst were studied, incorporating Co or Cu by coprecipitation or by incipient wetness impregnation. The experiments took place at 650°C and atmospheric pressure in a fixed bed and in a fluidized bed reactor, using an aqueous fraction (S/C=7.6molH2O/molC) of pine sawdust bio-oil. A spatial time (W/morg) of 4g catalyst min/g organics and an u/umf ratio of 10 (in fluidized bed) were used. In both reactors, the coprecipitated NiCo/AlMg catalyst showed the best performance. Over a period of 2h, 0.138g H2/g organics and 80% carbon conversion to gas were obtained in the fixed bed reactor. The catalyst deactivation rate was higher when the steam reforming took place in the fixed bed reactor, although the initial H2 and CO2 yields were higher. In contrast, the stability of the catalysts was higher in the fluidized bed reactor. Elemental analysis, FESEM and TPO analyses of some of the catalysts revealed a relationship between their stability and the quantity and characteristics of the coke deposited on their surface.},
keywords = {},
pubstate = {published},
tppubtype = {article}
}
An environmentally friendly method of producing a hydrogen rich gas is the catalytic steam reforming of bio-oil. This requires the development of a catalyst appropriate for the process. In the present work, five different research catalysts have been prepared and tested. A Ni/AlMg catalyst was selected as a reference. Modifications to the catalyst were studied, incorporating Co or Cu by coprecipitation or by incipient wetness impregnation. The experiments took place at 650°C and atmospheric pressure in a fixed bed and in a fluidized bed reactor, using an aqueous fraction (S/C=7.6molH2O/molC) of pine sawdust bio-oil. A spatial time (W/morg) of 4g catalyst min/g organics and an u/umf ratio of 10 (in fluidized bed) were used. In both reactors, the coprecipitated NiCo/AlMg catalyst showed the best performance. Over a period of 2h, 0.138g H2/g organics and 80% carbon conversion to gas were obtained in the fixed bed reactor. The catalyst deactivation rate was higher when the steam reforming took place in the fixed bed reactor, although the initial H2 and CO2 yields were higher. In contrast, the stability of the catalysts was higher in the fluidized bed reactor. Elemental analysis, FESEM and TPO analyses of some of the catalysts revealed a relationship between their stability and the quantity and characteristics of the coke deposited on their surface.
2012
Bimbela, Fernando; Chen, D; Ruiz, Joaquín; García, Lucía; Arauzo, Jesús
In: Applied Catalysis B: Environmental, vol. 119-120, pp. 1–12, 2012, ISSN: 09263373.
@article{Bimbela2012,
title = {Ni/Al coprecipitated catalysts modified with magnesium and copper for the catalytic steam reforming of model compounds from biomass pyrolysis liquids},
author = {Fernando Bimbela and D Chen and Joaquín Ruiz and Lucía García and Jesús Arauzo},
url = {http://www.sciencedirect.com/science/article/pii/S0926337312000628},
issn = {09263373},
year = {2012},
date = {2012-05-01},
journal = {Applied Catalysis B: Environmental},
volume = {119-120},
pages = {1--12},
abstract = {Ni/Al coprecipitated catalysts modified with magnesium and copper have been prepared by a constant pH technique and tested in the catalytic steam reforming of model compounds (acetic acid, acetol and butanol) from biomass pyrolysis liquids at 650°C and atmospheric pressure. Catalysts with different copper contents, reduced at 650°C for 1h, were tested in the steam reforming of acetic acid with a steam/carbon (S/C) molar ratio of 5.6. The best performance and the highest hydrogen yield in these conditions were achieved with the 5% Cu catalyst. This catalyst reduced at 650°C during 10h showed a high activity, close to the thermodynamic equilibrium, and a stable performance during 12h in the steam reforming of acetic acid with a S/C=5.6, using a short space time of 1.00g catalystmin/g acetic acid. Copper as a promoter produces counterbalanced effects: a decrease in the initial reforming activity and an enhancement of the catalyst stability. The initial steam reforming activity decreased and the CH4 yield increased concurrently with increasing the copper content, because of the Ni dilution effect. Copper has a positive effect inhibiting the formation of encapsulating coke, identified as the cause for deactivation in acetic acid steam reforming with a steam-to-carbon molar ratio (S/C) of 5.6. However, such a positive effect of copper has not been observed in acetic acid steam reforming with S/C=14.7 or in the steam reforming of acetol and butanol.},
keywords = {},
pubstate = {published},
tppubtype = {article}
}
Ni/Al coprecipitated catalysts modified with magnesium and copper have been prepared by a constant pH technique and tested in the catalytic steam reforming of model compounds (acetic acid, acetol and butanol) from biomass pyrolysis liquids at 650°C and atmospheric pressure. Catalysts with different copper contents, reduced at 650°C for 1h, were tested in the steam reforming of acetic acid with a steam/carbon (S/C) molar ratio of 5.6. The best performance and the highest hydrogen yield in these conditions were achieved with the 5% Cu catalyst. This catalyst reduced at 650°C during 10h showed a high activity, close to the thermodynamic equilibrium, and a stable performance during 12h in the steam reforming of acetic acid with a S/C=5.6, using a short space time of 1.00g catalystmin/g acetic acid. Copper as a promoter produces counterbalanced effects: a decrease in the initial reforming activity and an enhancement of the catalyst stability. The initial steam reforming activity decreased and the CH4 yield increased concurrently with increasing the copper content, because of the Ni dilution effect. Copper has a positive effect inhibiting the formation of encapsulating coke, identified as the cause for deactivation in acetic acid steam reforming with a steam-to-carbon molar ratio (S/C) of 5.6. However, such a positive effect of copper has not been observed in acetic acid steam reforming with S/C=14.7 or in the steam reforming of acetol and butanol.
2011
Bimbela, Fernando; Oliva, Miriam; Ruiz, Joaquín; García, Lucía; Arauzo, Jesús
Steam Reforming of Bio-Oil Aqueous Fractions for Syngas Production and Energy Journal Article
In: Environmental Engineering Science, vol. 28, no. 11, pp. 757–763, 2011, ISSN: 1092-8758.
@article{Bimbela2011,
title = {Steam Reforming of Bio-Oil Aqueous Fractions for Syngas Production and Energy},
author = {Fernando Bimbela and Miriam Oliva and Joaquín Ruiz and Lucía García and Jesús Arauzo},
url = {http://www.liebertpub.com/doi/10.1089/ees.2010.0367},
doi = {10.1089/ees.2010.0367},
issn = {1092-8758},
year = {2011},
date = {2011-11-01},
journal = {Environmental Engineering Science},
volume = {28},
number = {11},
pages = {757--763},
publisher = {Mary Ann Liebert, Inc. 140 Huguenot Street, 3rd Floor New Rochelle, NY 10801 USA},
abstract = {The biorefinery concept has been proposed as a route map to convert biomass into fuels and chemicals, maximizing economic and environmental benefits while minimizing pollution. A biorefinery strategy based on fast pyrolysis is proposed following a two-stage process, where biomass is first subjected to fast pyrolysis, optimized to collect up to 75% (per unit weight of biomass) of a liquid fraction called bio-oil. This bio-oil or its fractions can be upgraded in a second step to different chemicals, to a syngas and/or to energy. In particular, the catalytic steam reforming of the aqueous fraction of bio-oil obtained by fractionation with water is one of the most attractive possibilities for bio-oil upgrading, yielding a H2-rich syngas with low CO content. From the results obtained, it can be concluded that the best alternative for the catalytic steam reforming process is hydrogen production through further purification of the gas obtained. textcopyright 2011, Mary Ann Liebert, Inc.},
keywords = {},
pubstate = {published},
tppubtype = {article}
}
The biorefinery concept has been proposed as a route map to convert biomass into fuels and chemicals, maximizing economic and environmental benefits while minimizing pollution. A biorefinery strategy based on fast pyrolysis is proposed following a two-stage process, where biomass is first subjected to fast pyrolysis, optimized to collect up to 75% (per unit weight of biomass) of a liquid fraction called bio-oil. This bio-oil or its fractions can be upgraded in a second step to different chemicals, to a syngas and/or to energy. In particular, the catalytic steam reforming of the aqueous fraction of bio-oil obtained by fractionation with water is one of the most attractive possibilities for bio-oil upgrading, yielding a H2-rich syngas with low CO content. From the results obtained, it can be concluded that the best alternative for the catalytic steam reforming process is hydrogen production through further purification of the gas obtained. textcopyright 2011, Mary Ann Liebert, Inc.