Catalytic gasification of dry and wet biomass

Rossum, G. van; Potic, B.; Kersten, Sascha R.A.; Swaaij, W.P.M. van

doi:10.1016/j.cattod.2008.04.048

Cited by 74 publications

(46 citation statements)

References 46 publications

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“…This is believed to be the reason for the high carbon elutriation from an earlier used fluidized bed for steam reforming of pyrolysis oil. 3,7,8 The largest sizes of the spheres (around 100 micron) are in the same size range as the largest pyrolysis oil droplets (88-117 micron), which were photographed with the high speed camera. The spheres seem to be similar to the glassy/cenosphere solids produced during pyrolysis oil evaporation and/or combustion.…”

Section: Structural Analysis Of Charmentioning

confidence: 99%

Evaporation of pyrolysis oil: Product distribution and residue char analysis

et al. 2010

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The evaporation of pyrolysis oil was studied at varying heating rates (∼1–106°C/min) with surrounding temperatures up to 850°C. A total product distribution (gas, vapor, and char) was measured using two atomizers with different droplet sizes. It was shown that with very high heating rates (∼106°C/min) the amount of char was significantly lowered (∼8%, carbon basis) compared to the maximum amount, which was produced at low heating rates using a TGA (∼30%, carbon basis; heating rate 1°C/min). The char formation takes place in the 100–350°C liquid temperature range due to polymerization reactions of compounds in the pyrolysis oil. All pyrolysis oil fractions (whole oil, pyrolytic lignin, glucose and aqueous rich/lean phase) showed charring behavior. The pyrolysis oil chars age when subjected to elevated temperatures (≥700°C), show similar reactivity toward combustion and steam gasification compared with chars produced during fast pyrolysis of solid biomass. However, the structure is totally different where the pyrolysis oil char is very light and fluffy. To use the produced char in conversion processes (energy or syngas production), it will have to be anchored to a carrier. © 2010 American Institute of Chemical Engineers AIChE J, 2010

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Section: Structural Analysis Of Charmentioning

confidence: 99%

Evaporation of pyrolysis oil: Product distribution and residue char analysis

et al. 2010

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“…gasification and pyrolysis has already been developed [13,14,15]. Therefore, biomass gasification and pyrolysis-steam reforming for hydrogen production has drawn great interest, particularly using steam as the gasification agent and a suitable catalyst where the hydrogen yield can be significantly enhanced [16][17][18][19][20]. However, a challenge towards large scale commercialisation is tar formation in the product syngas and coke formation on the catalyst; the tar can block the pipework of downstream applications and the coke deposits on the surface of the reacted catalyst lead to deactivation [21].…”

Section: Introductionmentioning

confidence: 99%

Promoting hydrogen production and minimizing catalyst deactivation from the pyrolysis-catalytic steam reforming of biomass on nanosized NiZnAlOx catalysts

Dong

Ling

et al. 2017

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Hydrogen production from the thermochemical conversion of biomass was carried out with nano-sized NiZnAlOx catalysts using a two-stage fixed bed reactor system. The gases derived from the pyrolysis of wood sawdust in the first stage were catalytically steam reformed in the second stage. The NiZnAlOx catalysts were synthesized by a co-precipitation method with different Ni molar fractions (5, 10, 15, 25 and 35%) and a constant Zn:Al molar ratio of 1:4. The catalysts were characterized by a wide range of techniques, including N2 adsorption, SEM, XRD, TEM and temperature-programmed oxidation (TPO) and reduction (TPR). Fine metal particles of size around 10-11 nm were obtained and the catalysts had high stability characteristics, which improved the dispersion of active centers during the reaction and promoted the performance of the catalysts. The yield of gas was increased from 49.3 to 74.8 wt.%, and the volumetric concentration of hydrogen was increased from 34.7 to 48.1 vol.%, when the amount of Ni loading was increased from 5 to 35%. Meanwhile, the CH4 fraction decreased from 10.2 to 0.2 vol.% and the C2-C4 fraction was reduced from 2.4 vol.% to 0.0 vol.%. During the reaction, the crystal size of all catalysts was successfully maintained at around 10-11 nm with lowered catalyst coke formation, (particularly for the 35NiZn4Al catalyst where negligible coke was found) and additionally no obvious catalyst sintering was detected. The efficient production of hydrogen from the thermochemical conversion of renewable biomass indicates that it is a promising sustainable route to generate hydrogen from biomass using the NiZnAl metal oxide catalyst prepared in this work via a two-stage reaction system.

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“…However, the choice of the components of such surrogates is far from being obvious, and furthermore, such an approach will not allow the study of chemical kinetic interactions among bio-oil components. 4 are negligible. At lower temperature, the CH 4 and especially CO 2 contents increase.…”

Section: Thermochemistry and Equilibrium Calculationsmentioning

confidence: 95%