Auto-thermal reforming of acetic acid over hydrotalcites-derived co-based catalyst: A stable and anti-coking Co/Sr-Alx-O catalyst

Li, Huigu; Jia, Xuanyi; Wang, Ning; Chen, Baiquan; Xie, Xingyue; Qiao, Weihong; Huang, Lihong

doi:10.1016/j.apcatb.2019.118370

Cited by 25 publications

(12 citation statements)

References 60 publications

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“…The transformation pathway of HAc can be affected by the reaction temperature, which influences the distribution of the reaction products. As reported by Li et al [9], over CoSrAl-O catalysts tested in the range of 550-750 °C, the hydrogen HAc , while there were high selectivities to acetone and methane of up to 10 % and 18 %, respectively. To investigate the optimal reaction temperature during the ATR test, the CZP10 catalyst with high reactivity was further evaluated, as shown in Fig.…”

Section: Reactivity In Atr Of Hacsupporting

confidence: 72%

“…Furthermore, with the addition of Pr, the specific surface area and pore volume of the catalysts increased, and the CZP10 catalyst presented a relatively high specific surface area at 13.66 m 2 g −1 with an average pore size near 8.4 nm. However, over CZP30 with more Pr, the specific surface area decreased to 5.34 m 2 g −1 , which may be due to the destruction of the pore structure in the solid solution with excessive Pr 9, 27.…”

Section: Resultsmentioning

confidence: 96%

“…2) with Δ Η 0 = +131.4 kJ mol −1 and exothermic POX (Eq. 3) with Δ Η 0 = –350.6 kJ mol −1 , the heat equilibrium can be achieved by adjusting the feedstock ratio of O 2 /H 2 O to HAc 9, 10.

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + 1.4 {normalH}_{2} normalO + 0.28 {normalO}_{2} \to 2 normalC {normalO}_{2} + 3.44 {normalH}_{2} & center Δ H^{0} = 0 normal normalkJ normal normalmol^{- 1} \end{matrix}

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + 2 {normalH}_{2} normalO \to 2 normalC {normalO}_{2} + 4 {normalH}_{2} & center normalΔ H^{0} = normal normal+ normal 131 normal. 4 normal normalkJ normal normalmol^{- 1} \end{matrix}

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + {normalO}_{2} \to 2 normalC {normalO}_{2} + 2 {normalH}_{2} & center normalΔ H^{0} = - 350 normal. 6 normal normalkJ normal normalmol^{- 1} \end{matrix}

…”

Section: Introductionmentioning

confidence: 99%

“…( 2)) with ΔH 0 = +131.4 kJ mol -1 and exothermic POX (Eq. ( 3)) with ΔH 0 = -350.6 kJ mol -1 , the heat equilibrium can be achieved by adjusting the feedstock ratio of O 2 /H 2 O to HAc [9,10]. 1)…”

Section: Introductionmentioning

confidence: 99%

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Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

et al. 2022

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To obtain high yields of hydrogen, a series of Zr x Pr 1-x O y -supported cobalt catalysts were synthesized by the sol-gel method and tested in autothermal reforming (ATR) of acetic acid (HAc) derived from bio-oil. X-ray diffraction, nitrogen physisorption, H 2 -temperature-programmed reduction, and thermogravimetric analysis were conducted to investigate the factors affecting the activities of the catalysts. Over the Co-Zr-Pr-O catalyst, a Zr x Pr 1-x O y solid solution was formed after calcination; meanwhile, the active component of Co 0 was highly dispersed over the solid solution after reduction in hydrogen for 1 h at 700 °C. As a result, stable reactivity was recorded in the ATR process of HAc: the hydrogen yield reached 2.58 mol H2 mol À1HAc with near 100 % HAc conversion, while better resistance to coking was observed.

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Section: Reactivity In Atr Of Hacsupporting

confidence: 72%

Section: Resultsmentioning

confidence: 96%

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + 1.4 {normalH}_{2} normalO + 0.28 {normalO}_{2} \to 2 normalC {normalO}_{2} + 3.44 {normalH}_{2} & center Δ H^{0} = 0 normal normalkJ normal normalmol^{- 1} \end{matrix}

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + 2 {normalH}_{2} normalO \to 2 normalC {normalO}_{2} + 4 {normalH}_{2} & center normalΔ H^{0} = normal normal+ normal 131 normal. 4 normal normalkJ normal normalmol^{- 1} \end{matrix}

true \begin{matrix} center normalC {normalH}_{3} normalCOOH + {normalO}_{2} \to 2 normalC {normalO}_{2} + 2 {normalH}_{2} & center normalΔ H^{0} = - 350 normal. 6 normal normalkJ normal normalmol^{- 1} \end{matrix}

…”

Section: Introductionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

et al. 2022

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“…The research group of Huang, Wang, Xie and co-workers has been prolific in recent years in successfully investigating Ni, Co, Ni-Mn, Ni-Co based catalysts for ATR of HAc on various novel supports such as perovskites and double layered hydroxides at laboratory scale [10][11][12][13][14][15][16][17]. Steady conversion efficiencies (2.7-3 mol H 2 /mol HAc.)…”

Section: Introductionmentioning

confidence: 99%

Autothermal Reforming of Acetic Acid to Hydrogen and Syngas on Ni and Rh Catalysts

et al. 2021

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The autothermal reforming (ATR) of acetic acid (HAc) as a model bio-oil compound is examined via bench scale experiments and equilibrium modelling to produce hydrogen and syngas. This study compares the performance of nickel (Ni-Al, Ni-CaAl) vs. rhodium (Rh-Al) for particulate packed bed (PPB), and of Rh-Al in PPB vs. Rh with and without Ceria for honeycomb monolith (‘M’) catalysts (R-M and RC-M). All PPB and M catalysts used Al2O3 as main support or washcoat, and when not pre-reduced, exhibited good performance with more than 90% of the HAc converted to C1-gases. The maximum H2 yield (6.5 wt.% of feed HAc) was obtained with both the Rh-Al and Ni-CaAl catalysts used in PPB, compared to the equilibrium limit of 7.2 wt.%, although carbon deposition from Ni-CaAl at 13.9 mg gcat−1 h−1 was significantly larger than Rh-Al’s (5.5 mg gcat−1 h−1); close to maximum H2 yields of 6.2 and 6.3 wt.% were obtained for R-M and RC-M respectively. The overall better performance of the Ni-CaAl catalyst over that of the Ni-Al was attributed to the added CaO reducing the acidity of the Al2O3 support, which provided a superior resistance to persistent coke formation. Unlike Rh-Al, the R-M and RC-M exhibited low steam conversions to H2 and CH4, evidencing little activity in water gas shift and methanation. However, the monolith catalysts showed no significant loss of activity, unlike Ni-Al. Both catalytic PPB (small reactor volumes) and monolith structures (ease of flow, strength, and stability) offer different advantages, thus Rh and Ni catalysts with new supports and structures combining these advantages for their suitability to the scale of local biomass resources could help the future sustainable use of biomasses and their bio-oils as storage friendly and energy dense sources of green hydrogen.

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Hydrogen Production through Distinctive C−C Cleavage during Acetic Acid Reforming at Low Temperature

Shen,

Yang,

Tang

et al. 2024

ChemSusChem

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Acetic acid reforming is a green method for sustainable hydrogen production owing to its renewable source from biomass conversion. However, conventional acetic acid reforming would produce various byproducts, including CO, CH4 and so on. Here, we develop a distinctive method for selective hydrogen production from C‐C directional cleavage during acetic acid reforming. Completely different from conventional acetic acid reforming process, acetic acid would react with water over organoruthenium catalyst during its C‐C cleavage at low temperature, then produce methanol and formic acid (CH3COOH+H2O→CH3OH+HCOOH). Lastly, methanol and formic acid could further decompose into hydrogen and carbon dioxide over organoruthenium selectively.Hydrogen production rate is up to 26.8 molH2/(h‐1*mol‐1Ru) at 150 ℃ through a tandem catalysis. A mechanism for C‐C cleavage of acetic acid is proposed based on intermediate product analysis and density functional theory (DFT) calculation. Firstly, the C‐C single bond was transformed into C=C double bond by dropping one H atom to organoruthenium. Then the coming H2O molecule reacted with the C=C bond by an addition reaction, forming methanol and formic acid. This research not only proposes distinctive reaction pathway for hydrogen production from acetic acid reforming, but also provides some inspiration for selective C‐C bond cleavage during ethanol reforming.

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Auto-thermal reforming of acetic acid over hydrotalcites-derived co-based catalyst: A stable and anti-coking Co/Sr-Alx-O catalyst

Cited by 25 publications

References 60 publications

Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

Autothermal Reforming of Acetic Acid to Hydrogen and Syngas on Ni and Rh Catalysts

Hydrogen Production through Distinctive C−C Cleavage during Acetic Acid Reforming at Low Temperature

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Auto-thermal reforming of acetic acid over hydrotalcites-derived co-based catalyst: A stable and anti-coking Co/Sr-Alx-O catalyst

Cited by 25 publications

References 60 publications

ZrxPr1–xOy Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

ZrxPr1–xOy Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

Autothermal Reforming of Acetic Acid to Hydrogen and Syngas on Ni and Rh Catalysts

Hydrogen Production through Distinctive C−C Cleavage during Acetic Acid Reforming at Low Temperature

Contact Info

Product

Resources

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Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production

Zr_xPr_1–xO_y Solid Solution‐Supported Cobalt‐Based Catalysts for Hydrogen Production