Hydrogen production via acetic acid steam reforming: A critical review on catalysts

Chen, Guanyi; Tao, Junyu; Liu, Caixia; Yan, Beibei; Li, Wanqing; Li, Xiangping

doi:10.1016/j.rser.2017.05.107

Cited by 124 publications

(51 citation statements)

References 126 publications

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“…Thus, the bio-oil produced in decentralised pyrolysis units can be subsequently transported to a centralized unit for H 2 production. This transport is more economical than that of the biomass, due to the higher density of bio-oil [13]. Compared to other routes for valorising bio-oil, steam reforming has the additional advantage that it does not require water separation.…”

Section: Introductionmentioning

confidence: 99%

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

et al. 2018

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Several Ni catalysts of supported (on La 2 O 3 -αAl 2 O 3 , CeO 2 , and CeO 2 -ZrO 2 ) or bulk types (Ni-La perovskites and NiAl 2 O 4 spinel) have been tested in the oxidative steam reforming (OSR) of raw bio-oil, and special attention has been paid to the catalysts' regenerability by means of studies on reaction-regeneration cycles. The experimental set-up consists of two units in series, for the separation of pyrolytic lignin in the first step (at 500 • C) and the on line OSR of the remaining oxygenates in a fluidized bed reactor at 700 • C. The spent catalysts have been characterized by N 2 adsorption-desorption, X-ray diffraction and temperature programmed reduction, and temperature programmed oxidation (TPO). The results reveal that among the supported catalysts, the best balance between activity-H 2 selectivity-stability corresponds to Ni/La 2 O 3 -αAl 2 O 3 , due to its smaller Ni 0 particle size. Additionally, it is more selective to H 2 than perovskite catalysts and more stable than both perovskites and the spinel catalyst. However, the activity of the bulk NiAl 2 O 4 spinel catalyst can be completely recovered after regeneration by coke combustion at 850 • C because the spinel structure is completely recovered, which facilitates the dispersion of Ni in the reduction step prior to reaction. Consequently, this catalyst is suitable for the OSR at a higher scale in reaction-regeneration cycles.

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Section: Introductionmentioning

confidence: 99%

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

et al. 2018

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“…Lower temperature (below 550°C) can generate coke due to Boudouard reaction Equation and the reverse of carbon gasification Equation . In contrast, higher temperature (above 600°C) easily takes methane decomposition reaction Equation which is the domain process . The type of amorphous coke deposition easily formed at low temperature while oligomeric coke is contrary .…”

Section: Resultsmentioning

confidence: 99%

“…Hydrogen is considered as an environmental‐friendly energy, because hydrogen is zero emission upon combustion and has a high weight‐based energy density . The specific energy of hydrogen (143 kJ kg −1 ) is up to three times larger than most liquid hydrocarbon‐based fuel . Hydrogen is traditionally produced from carbonaceous fuel, such as coal, natural gas, oil, and biomass .…”

Section: Introductionmentioning

confidence: 99%

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Hydrogen‐rich syngas production from chemical looping steam reforming of bio‐oil model compound: Effect of bimetal on LaNi _0.8 M _0.2 O ₃ (M = Fe, Co, Cu, and Mn)

2019

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Summary Chemical looping steam reforming (CLSR) of acetic acid as bio‐oil model compound is a suitable way to produce hydrogen‐rich syngas. The LaNiO3 and LaNi0.8M0.2O3 (M = Fe, Co, Mn, and Cu) perovskites were prepared via the sol‐gel method. The perovskites were characterized by X‐ray diffraction (XRD), thermogravimetry (TG), and test activity of hydrogen‐rich syngas in a fixed bed. XRD and TG results showed that the coke generation on LaNi0.8Fe0.2O3 needs a lower decomposition temperature, and a stable structure was appeared after reaction. The activity order of hydrogen‐rich syngas on five types of perovskite is LaNi0.8Fe0.2O3 > LaNi0.8Co0.2O3 > LaNiO3 > LaNi0.8Mn0.2O3 > LaNi0.8Cu0.2O3 at 650°C, mole ratio of steam/carbon (2:1), and sample mixture flow (GHSV = 34 736 g of feed/(g catalyst h)). The CLSR of acetic acid with LaNi0.8Fe0.2O3 at GHSV = 43 992 g of feed/(g catalyst h) showed good stability. Correlated to experimental results, the adsorption energy of steam and acetic acid on five types of perovskite were calculated using density functional theory (DFT). The adsorption energy of steam (−0.61 eV) and acetic acid (−0.93 eV) of LaNi0.8Fe0.2O3 is maximum. This value of DFT calculation is well explained in the experimental results.

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“…This is due to the complex distribution of components changes with the biomass precursor and pyrolysis parameters. Acetic acid (HAc) is one of the major carboxylic acid compounds in bio‐oil with a concentration up to 10–12 wt% . Hydrogen production from steam reforming of HAc leads to the formation of H 2 between 70–80% .…”

Section: Introductionmentioning

confidence: 99%

Investigation on Co–Modified Ni_xMg_yO Solid Solutions for Hydrogen Production from Steam Reforming of Acetic Acid and a Model Blend

et al. 2019

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This paper is focused on the Co‐modified NixMgyO solid solutions (10 wt% Ni, 2–6 wt% Co) for the steam reforming of acetic acid and a model blend. The pristine rocksalt structured NixMgyO solid solution and the modified NixMgyO−Co catalysts were synthesized via hydrothermal method and co‐impregnation. The activity of the catalysts was evaluated in the temperature range of 500–800 °C with a steam/carbon molar ratio of 3 and a gas hourly space velocity (GHSV) of 57,000 h−1. Low cobalt content (Co loading= 2 wt%) catalysts exhibited significant promotion of H2 yield via enhancement of both water‐gas shift (WGS) reaction and methane decomposition. A 30‐hour test at 700 °C achieved excellent acetic acid conversion rate and H2 yield of 99.1% and 86.9%, respectively. However, the catalysts with higher cobalt loading (Co loading≥ 4 wt%) suffered a much quicker deactivation mainly due to carbon deposition. In addition, the catalysts were also tested on a model blend combined acids, alcohols and aromatic species and exhibited outstanding performance with carbon conversion above 90% and H2 yield above 70% for 100 h.

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Hydrogen production via acetic acid steam reforming: A critical review on catalysts

Cited by 124 publications

References 126 publications

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

Hydrogen‐rich syngas production from chemical looping steam reforming of bio‐oil model compound: Effect of bimetal on LaNi _0.8 M _0.2 O ₃ (M = Fe, Co, Cu, and Mn)

Investigation on Co–Modified Ni_xMg_yO Solid Solutions for Hydrogen Production from Steam Reforming of Acetic Acid and a Model Blend

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Hydrogen production via acetic acid steam reforming: A critical review on catalysts

Cited by 124 publications

References 126 publications

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

Oxidative Steam Reforming of Raw Bio-Oil over Supported and Bulk Ni Catalysts for Hydrogen Production

Hydrogen‐rich syngas production from chemical looping steam reforming of bio‐oil model compound: Effect of bimetal on LaNi 0.8 M 0.2 O 3 (M = Fe, Co, Cu, and Mn)

Investigation on Co–Modified NixMgyO Solid Solutions for Hydrogen Production from Steam Reforming of Acetic Acid and a Model Blend

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Product

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Hydrogen‐rich syngas production from chemical looping steam reforming of bio‐oil model compound: Effect of bimetal on LaNi _0.8 M _0.2 O ₃ (M = Fe, Co, Cu, and Mn)

Investigation on Co–Modified Ni_xMg_yO Solid Solutions for Hydrogen Production from Steam Reforming of Acetic Acid and a Model Blend