Hydrogenation of CO2 over sprayed Ru/TiO2 fine particles and strong metal–support interaction

Li, Di; Ichikuni, Nobuyuki; Shimazu, Shogo; Uematsu, Takayoshi

doi:10.1016/s0926-860x(98)00335-4

Cited by 106 publications

(52 citation statements)

References 38 publications

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“…It is clear that the support has a significant influence on the catalytic activity and selectivity. Generally, a strong metal-support interaction exists in the supported noble metal catalysts, and it will affect the performance of the active species greatly, such as for the TiO 2 -supported catalysts: the electron density around the metal particles decreased as the electron transferred (or polarized) from the metal nanoparticle to TiO 2 [28][29][30], and the electron-deficient state of the metal nanoparticle is favorable for the adsorption or hydrogenation of the nitro group [30][31][32]. Furthermore, the support has a great influence on the adsorption and desorption of the substrates, intermediates and products.…”

Section: Resultsmentioning

confidence: 99%

Selective Hydrogenation of m-Dinitrobenzene to m-Nitroaniline over Ru-SnOx/Al2O3 Catalyst

Cheng

Lin

et al. 2014

Catalysts

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Series catalysts of Ru-SnO x /Al 2 O 3 with varying SnO x loading of 0-3 wt% were prepared, and their catalytic activity and selectivity have been discussed and compared for the selective hydrogenation of m-dinitrobenzene (m-DNB) to m-nitroaniline (m-NAN). The Ru-SnO x /Al 2 O 3 catalysts were characterized by X-ray powder diffraction (XRD), X-ray photoelectron spectroscopy (XPS), transmission electron microscopy (TEM) and hydrogen temperature-programmed reduction (H 2 -TPR) and desorption (H 2 -TPD). Under the modification of SnO x , the reaction activity increased obviously, and the best selectivity to m-NAN reached above 97% at the complete conversion of m-DNB. With the increasing of the SnO x loading, the amount of active hydrogen adsorption on the surface of the catalyst increased according to the H 2 -TPD analysis, and the electron transferred from Ru to SnO x species, as determined by XPS, inducing an electron-deficient Ru, which is a benefit for the absorption of the nitro group. Therefore, the reaction rate and product selectivity were greatly enhanced. Moreover, the Ru-SnO x /Al 2 O 3 catalyst presented high stability: it could be recycled four times without any loss in activity and selectivity.

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Section: Resultsmentioning

confidence: 99%

Selective Hydrogenation of m-Dinitrobenzene to m-Nitroaniline over Ru-SnOx/Al2O3 Catalyst

Cheng

Lin

et al. 2014

Catalysts

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“…Its catalytic activity and selectivity to CH 4 are, however, largely dependent on the dispersion of the metallic phase (at high dispersion the apparent activation energy reaches a minimum), on the type of the support, and an addition of modifiers/promoters that can more or less chemically interact with the metal [45][46][47][48][49][50][51][52][53][54] [55,56]. The activity of pre-reduced 3%Ru/Al 2 O 3 catalyst (CO 2 conversion, CH 4 and CO yields), as a function of the reaction temperature, is reported in Figure 4 [53].…”

Section: Rutheniummentioning

confidence: 99%

Supported Catalysts for CO2 Methanation: A Review

et al. 2017

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CO 2 methanation is a well-known reaction that is of interest as a capture and storage (CCS) process and as a renewable energy storage system based on a power-to-gas conversion process by substitute or synthetic natural gas (SNG) production. Integrating water electrolysis and CO 2 methanation is a highly effective way to store energy produced by renewables sources. The conversion of electricity into methane takes place via two steps: hydrogen is produced by electrolysis and converted to methane by CO 2 methanation. The effectiveness and efficiency of power-to-gas plants strongly depend on the CO 2 methanation process. For this reason, research on CO 2 methanation has intensified over the last 10 years. The rise of active, selective, and stable catalysts is the core of the CO 2 methanation process. Novel, heterogeneous catalysts have been tested and tuned such that the CO 2 methanation process increases their productivity. The present work aims to give a critical overview of CO 2 methanation catalyst production and research carried out in the last 50 years. The fundamentals of reaction mechanism, catalyst deactivation, and catalyst promoters, as well as a discussion of current and future developments in CO 2 methanation, are also included.

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“…The catalyst was prepared by incipient wetness impregnation, following literature procedures [28][29][30][31][32]. The support was impregnated with the adequate amount of the precursor aqueous solution and dried at 110 °C for 24 h. Then the sample was crushed and oxidized at 500 °C for 4 h, reduced with hydrogen at 400 °C for 5 h, cooled to room temperature under nitrogen and stored in caped vials until use.…”

Section: Preparation and Characterization Of The Ru/zro 2 Catalystmentioning

confidence: 99%

Catalytic gasification of glycerol in supercritical water

May

Salvadó

Torras

et al. 2010

Chemical Engineering Journal

100

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The conversion of glycerol in supercritical water (SCW) was studied at 510 -550°C and a pressure of 350 bars using both a bed of inert and non-porous ZrO 2 particles (hydrothermal experiments), and a bed of 1 % Ru/ZrO 2 catalyst particles. Experiments were conducted with a glycerol concentration of 5 wt% in a continuous isothermal fixed-bed reactor at a residence time between 2 and 10 s. Hydrothermolysis of glycerol formed water-soluble products such as acetaldehyde, acetic acid, hydroxyacetone and acrolein, and also gases like H 2 , CO and CO 2 .The catalyst enhanced the formation of acetic acid, inhibited the formation of acrolein, and promoted the gasification of the glycerol decomposition products. Hydrogen and carbon oxides were the main gases produced in the catalytic experiments, with only minor amounts of methane and ethylene. Complete glycerol conversion was achieved at a residence time of 8.5 s at 510 °C, and at around 5 s at 550 °C with a 1 wt% Ru/ZrO 2 catalyst. The catalyst was not active enough to achieve complete gasification, since high yields of primary products like acetic acid and acetaldehyde were still present. Carbon balances were between 80 and 60 % in the catalytic experiments, decreasing continuously as the residence time was increased. This was attributed partially to the formation of methanol and acetaldehyde, which were not recovered and analyzed efficiently in our set-up, but also to the formation of carbon deposits. Carbon deposition was not observed on the catalyst particles but on the surface of the inert zirconia particles, especially at high residence time. This was related to the higher concentration of acetic acid and other acidic species in the catalytic experiments, which may polymerize to form tar-like carbon precursors. Because of carbon deposition, hydrogen yields were significantly lower than expected; for instance at 550 ºC the hydrogen yield potential was only 50 % of the stoichiometric value.

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Hydrogenation of CO2 over sprayed Ru/TiO2 fine particles and strong metal–support interaction

Cited by 106 publications

References 38 publications

Selective Hydrogenation of m-Dinitrobenzene to m-Nitroaniline over Ru-SnOx/Al2O3 Catalyst

Selective Hydrogenation of m-Dinitrobenzene to m-Nitroaniline over Ru-SnOx/Al2O3 Catalyst

Supported Catalysts for CO2 Methanation: A Review

Catalytic gasification of glycerol in supercritical water

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