Lucía García

@article{Remon2016g,

title = {Bio-oil upgrading in supercritical water using Ni-Co catalysts supported on carbon nanofibres},

author = {Javier Remón and Jesús Arauzo and Lucía García and P Arcelus-Arrillaga and M Millan and Isabel Suelves and J L Pinilla},

doi = {10.1016/j.fuproc.2016.08.030},

issn = {03783820},

year  = {2016},

date = {2016-12-01},

journal = {Fuel Processing Technology},

volume = {154},

pages = {178--187},

publisher = {Elsevier B.V.},

abstract = {This work addresses the preparation, characterisation and screening of different Ni-Co catalysts supported on carbon nanofibres (CNFs) for use in the upgrading of bio-oil in supercritical water. The aim is to improve the physicochemical properties of bio-oil so that it can be used as a fuel. The CNFs were firstly oxidised in HNO3 and afterwards subjected to a thermal treatment to selectively modify their surface chemistry prior to the incorporation of the metal active phase (Ni-Co). The CNFs and the supported catalysts were thoroughly characterised by several techniques, which allowed a relationship to be established between the catalyst properties and the upgrading results. The use of Ni-Co/CNFs for bio-oil upgrading in supercritical water (SCW) significantly improved the properties of the original feedstock. In addition, the thermal treatment to which the fibres were subjected exerted a significant influence on their catalytic properties. An increase in the severity of the thermal treatment led to a substantial reduction in the oxygen content of the CNFs, mainly due to the removal of the less stable oxygen surface groups, which allowed their surface polarity to decrease. This decrease resulted in less formation of solid products. However, it also reduced the H/C and increased the O/C ratios of the upgraded liquid. Therefore, a compromise between the yield and the properties of the upgraded bio-oil was achieved with a Ni-Co supported on a CNF with a moderate amount of oxygen surface groups.},

keywords = {},

pubstate = {published},

tppubtype = {article}

}

@article{Remon2016e,

title = {Cheese whey management by catalytic steam reforming and aqueous phase reforming},

author = {Javier Remón and Lucía García and Jesús Arauzo},

doi = {10.1016/j.fuproc.2016.08.012},

issn = {03783820},

year  = {2016},

date = {2016-12-01},

journal = {Fuel Processing Technology},

volume = {154},

pages = {66--81},

publisher = {Elsevier B.V.},

abstract = {Cheese whey is a yellowish liquid by-product of the cheese making process. Owing to its high BOD and COD values, this feedstock should not be directly discharged into the environment without appropriate treatment. The management of this wastewater has become an important issue, and new treatments must be sought. This work addresses the valorisation of cheese whey by steam reforming and aqueous phase reforming. The catalytic steam reforming of cheese whey turned out to be a promising valorisation route for H2 production from this effluent. This process enabled the organic compounds present in the cheese whey to be transformed into a rich H2 gas (35% of the C of the feed was transformed into a gas with 70 vol.% of H2). This significantly reduced the amount of carbon present in the original feedstock, producing an almost carbon-free liquid stream. The aqueous phase reforming of cheese whey allowed 35% of the carbon present in the whey to be transformed into gases and 45% into valuable liquids. The gas was principally made up of H2 and CO2, while a mixture of added-value liquids such as aldehydes, carboxylic acids, alcohols and ketones constituted the liquid phase. However, both valorisation routes produced a substantial amount of solid. The formation of this solid was promoted by the presence of salts in the original feedstock and caused operational problems for both valorisation processes. In addition, it hampered gas production in the case of steam reforming and reduced gas and liquid formation when using aqueous phase reforming as the valorisation route. The filtration of cheese whey slightly decreased the solid formation in both processes due to the reduction of proteins and fats, both of which partly contribute to such formation. Less solid was formed in the experiments conducted with lactose than in those conducted with whole and with filtered cheese whey.},

keywords = {},

pubstate = {published},

tppubtype = {article}

}

@article{Remon2016a,

title = {Effect of biodiesel-derived impurities (acetic acid, methanol and potassium hydroxide) on the aqueous phase reforming of glycerol},

author = {Javier Remón and Joaquín Ruiz and Miriam Oliva and Lucía García and Jesús Arauzo},

doi = {10.1016/j.cej.2016.05.018},

issn = {13858947},

year  = {2016},

date = {2016-09-01},

journal = {Chemical Engineering Journal},

volume = {299},

pages = {431--448},

publisher = {Elsevier B.V.},

abstract = {This work analyses the influence of three biodiesel-derived impurities (CH3OH, CH3COOH and KOH) on the aqueous phase reforming of glycerol at 220 °C and 44 bar using a Ni-La/Al2O3 catalyst. The experiments were planed according to a factorial 2k design and analysed by means of an analysis of variance (ANOVA) test to identify the effect of each impurity and all possible binary and ternary combinations. The presence of CH3OH decreased the glycerol conversion, while CH3COOH and KOH decreased and increased the gas production, respectively. Catalyst deactivation took place under acidic conditions due to the loss of part of the active phase of the catalyst through leaching. The gas phase was made up of H2, CO2, CO and CH4. KOH exerted the greatest influence on the gas composition, increasing H2 production due to the greater gas production and the lower H2 consumption in the hydrogenation reactions. The liquid phase was made up of aldehydes, monohydric and polyhydric alcohols, C3 and C4 ketones and esters. CH3OH increased the proportion of monohydric alcohols, while CH3COOH promoted dehydration reactions, leading to an increase in the relative amount of C3-ketones.},

keywords = {},

pubstate = {published},

tppubtype = {article}

}

@article{Remon2016h,

title = {Cheese whey valorisation: Production of valuable gaseous and liquid chemicals from lactose by aqueous phase reforming},

author = {Javier Remón and Joaquín Ruiz and Miriam Oliva and Lucía García and Jesús Arauzo},

doi = {10.1016/j.enconman.2016.07.044},

issn = {01968904},

year  = {2016},

date = {2016-09-01},

journal = {Energy Conversion and Management},

volume = {124},

pages = {453--469},

publisher = {Elsevier Ltd},

abstract = {Cheese effluent management has become an important issue owing to its high biochemical oxygen demand and chemical oxygen demand values. Given this scenario, this work addresses the valorisation of lactose (the largest organic constituent of this waste) by aqueous phase reforming, analysing the influence of the most important operating variables (temperature, pressure, lactose concentration and mass of catalyst/lactose mass flow rate ratio) as well as optimising the process for the production of either gaseous or liquid value-added chemicals. The carbon converted into gas, liquid and solid products varied as follows: 5–41%, 33–97% and 0–59%, respectively. The gas phase was made up of a mixture of H2 (8–58 vol.%), CO2 (33–85 vol.%), CO (0–15 vol.%) and CH4 (0–14 vol.%). The liquid phase consisted of a mixture of aldehydes: 0–11%, carboxylic acids: 0–22%, monohydric alcohols: 0–23%, polyhydric-alcohols: 0–48%, C3-ketones: 4–100%, C4-ketones: 0–18%, cyclic-ketones: 0–15% and furans: 0–85%. H2 production is favoured at high pressure, elevated temperature, employing a high amount of catalyst and a concentrated lactose solution. Liquid production is preferential using diluted lactose solutions. At high pressure, the production of C3-ketones is preferential using a high temperature and a low amount of catalyst, while a medium temperature and a high amount of catalyst favours the production of furans. The production of alcohols is preferential using medium temperature and pressure and a low amount of catalyst.},

keywords = {},

pubstate = {published},

tppubtype = {article}

}

@article{Remon2016f,

title = {Production of gaseous and liquid bio-fuels from the upgrading of lignocellulosic bio-oil in sub- and supercritical water: Effect of operating conditions on the process},

author = {Javier Remón and P Arcelus-Arrillaga and Lucía García and Jesús Arauzo},

doi = {10.1016/j.enconman.2016.04.010},

issn = {01968904},

year  = {2016},

date = {2016-07-01},

journal = {Energy Conversion and Management},

volume = {119},

pages = {14--36},

publisher = {Elsevier Ltd},

abstract = {This work analyses the influence of the temperature (310-450 °C), pressure (200-260 bar), catalyst/bio-oil mass ratio (0-0.25 g catalyst/g bio-oil), and reaction time (0-60 min) on the reforming in sub- and supercritical water of bio-oil obtained from the fast pyrolysis of pinewood. The upgrading experiments were carried out in a batch micro-bomb reactor employing a co-precipitated Ni-Co/Al-Mg catalyst. This reforming process turned out to be highly customisable for the valorisation of bio-oil for the production of either gaseous or liquid bio-fuels. Depending on the operating conditions and water regime (sub/supercritical), the yields to upgraded bio-oil (liquid), gas and solid varied as follows: 5-90%, 7-91% and 3-31%, respectively. The gas phase, having a LHV ranging from 2 to 17 MJ/m3 STP, was made up of a mixture of H2 (9-31 vol.%), CO2 (41-84 vol.%), CO (1-22 vol.%) and CH4 (1-45 vol.%). The greatest H2 production from bio-oil (76% gas yield with a relative amount of H2 of 30 vol.%) was achieved under supercritical conditions at a temperature of 339 °C, 200 bar of pressure and using a catalyst/bio-oil ratio of 0.2 g/g for 60 min. The amount of C, H and O (wt.%) in the upgraded bio-oil varied from 48 to 74, 4 to 9 and 13 to 48, respectively. This represents an increase of up to 37% and 171% in the proportions of C and H, respectively, as well as a decrease of up to 69% in the proportion of O. The HHV of the treated bio-oil shifted from 20 to 35 MJ/kg, which corresponds to an increase of up to 89% with respect to the HHV of the original bio-oil. With a temperature of around 344 °C, a pressure of 233 bar, a catalyst/bio-oil ratio of 0.16 g/g and a reaction time of 9 min a compromise was reached between the yield and the quality of the upgraded liquid, enabling the transformation of 62% of the bio-oil into liquid with a HHV (29 MJ/kg) about twice as high as that of the original feedstock (17 MJ/kg).},

keywords = {},

pubstate = {published},

tppubtype = {article}

}