Experimental Investigation on Upgrading of Lignin‐Derived Bio‐Oils: Kinetic Analysis of Anisole Conversion on Sulfided CoMo/Al₂O₃ Catalyst

Abstract

Kinetics of the hydroprocessing of anisole, a compound representative of lignin-derived bio-oils, catalyzed by a commercial sulfided CoMo/Al2O3 were determined at 8-20 bar pressure and 573-673 K with a once-through flow reactor. The catalyst was sulfided in an atmosphere of H2 + H2S prior to the measurement of its performance. Selectivity-conversion data were used as a basis for determining an approximate, partially quantified reaction network showing that hydrodeoxygenation, hydrogenolysis, and alkylation reactions take place simultaneously. The data indicate that these reactions can be stopped at the point where HDO is virtually completed and hydrogenation reactions (and thus H2 consumption) are minimized. Phenol was the major product of the reactions, with direct deoxygenation of anisole to give benzene being kinetically almost insignificant under our conditions. We infer that the scission of the Cmethyl-O bond is

Kinetic Modeling and Experimental Investigation of Hydro‐Catalytic Upgrading of Anisole as a Model Compound of Bio‐Oils Derived from Fast Pyrolysis of Lignin over Co/γ‐Al2O3

“…Besides, the comparison of formation rates over Co/γ-Al 2 O 3 with the commercial CoMo/γ-Al 2 O 3 catalyst is also presented in Table 1. [32] Evaluation of represented data infers that the rate of hydrogenolysis, alkylation and transalkylation reactions over Co/γ-Al 2 O 3 at different temperatures is higher than those over the commercial CoMo/γ-Al 2 O 3 catalyst. In contrast, commercial CoMo/γ-Al 2 O 3 catalyst is more favorable than Co/γ-Al 2 O 3 catalyst for HDO reaction which this can be attributed to the effect of Mo active phase.…”

“…Furthermore, it is notable that the overall rate of anisole conversion over Co/γ-Al 2 O 3 at higher temperatures is more that over the commercial CoMo/γ-Al 2 O 3 catalyst in which over the latter the overall rate was 5.26 × 10 À 3 , 8.54 × 10 À 3 , and 1.28 × 10 À 2 (mol/(g of catalyst × h) at 573, 623 and 673 K, respectively. [32] To determine the rate constants of products formation, plots of (1-X i ) (where X i is the conversion of anisole to the species of i) on a logarithmic scale versus inverse WHSV were generated. Eqs.…”

The utilization of synthesis gas for the deoxygenation of cyclohexanone over alumina‐supported catalysts: Screening catalysts

“…The utilized microflow reactor (Microactivity‐Reference, PID Eng & Tech) for the conversion of cyclohexanone has been well introduced in the previous studies . A fixed‐bed once‐through tubular reactor working in the down‐flow mode and equipped with a porous plate for the catalyst particles was utilized.…”

“…Liquid products were then collected and analyzed. More information about the reaction system could be found elsewhere . The experimental setup is sketched in Figure .…”

Fine-Tuning Synthesis and Characterization of Mono-Sized H-Beta Zeolite-Supported Palladium-Iridium Nanoparticles and Application in the Selective Hydrogenation of Acetylene

“…Both findings indicate that virtually no Pd leaches from the surface into the solution. Figure 15 demonstrates a schematic plan of the apparatus, including a fixed-bed cylindrical microactivity-reactor acting in down-flow procedure, with the catalyst fixed-bed placed on a poriferous plate [85][86][87][88][89]. The microactivity-reactor was placed inside a hot box (304 stainless steel) insulated with heating capability to 220 • C. A thermocouple with K type encrusted with a 1.5 mm thickness and Inconel covering was placed horizontally via up to down of the micro-activity reactor and was in straight connection with the fixed bed.…”