02735nas a2200169 4500008004100000022001400041245012600055210006900181260000800250300001400258490000700272520210000279100001702379700001702396700002502413856012702438 2022 eng d a1463-926200aReview on non-noble metal catalysts for glycerol hydrodeoxygenation to 1,2-propanediol with and without external hydrogen0 aReview on nonnoble metal catalysts for glycerol hydrodeoxygenati cSEP a6751-67810 v243 a

The depleting petroleum oil resources, political embargos, and global warming dilemma have made it mandatory to develop alternative green technologies for energy and chemical production. Glycerol is one of the top-12 building block chemicals that can be mainly obtained as a coproduct of biodiesel production. The value addition of glycerol is only possible through its conversion to commodity and fine chemicals. Glycerol hydrogenolysis is one of the crucial pathways to produce several value-added products, among which 1,2-propanediol (1,2-PDO), 1,3-propanediol (1,3-PDO), ethylene glycol (EG) and 1-and/or 2-propanols are hydrogenolysis products. Selective glycerol hydrogenolysis to the desired product 1,2-PDO is only possible through the catalyst having an optimum combination of acid/base and metal sites (metallic and mixed oxides). The present review mainly focuses on the critical assessment of the influence of different supports, catalyst preparation methods, and/or pretreatment on structural, and electronic properties and simultaneously on the activity and product selectivity of non-noble metal catalysts. The role of reaction parameters in this industrially important reaction on catalyst performance will also be presented. A rigorous survey of patented literature on non-noble metal-catalyzed glycerol hydrogenolysis to 1,2-PDO is also discussed. Further, the review covers recent progress on non-noble metal-catalyzed autogenous glycerol hydrogenolysis through glycerol aqueous phase reforming (APR) and/or catalytic transfer hydrogenolysis (CTH), to overcome the cost and handling issues of external hydrogen. Finally, techno-economic analysis is also presented which compares the glycerol hydrogenolysis with and without external hydrogen with the conventional process of 1,2-PDO production. This analysis indicated that CTH and glycerol hydrogenolysis under ambient hydrogen pressure have the potential for commercialization, however catalyst stability and elimination of co-product formation at higher glycerol concentration need to be considered critically.

1 aMane, Rasika1 aJeon, Yukwon1 aRode, Chandrashekhar uhttps://library.ncl.res.in/content/review-non-noble-metal-catalysts-glycerol-hydrodeoxygenation-12-propanediol-and-without04129nas a2200169 4500008004100000245013600041210006900177260000800246300001200254490000700266520348100273100001703754700001903771700001703790700002503807856012703832 2024 eng d00aCalcination temperature impacting the structure and activity of CuAl catalyst in aqueous glycerol hydrogenolysis to 1,2-propanediol0 aCalcination temperature impacting the structure and activity of  cNOV a318-3310 v683 a

This study investigated the impact of calcination temperature on the structural properties of CuAl catalyst which was found to be a robust nano-structured catalyst calcined directly without ramping at 400 °C and performed exceedingly well for aqueous phase hydrogenolysis of glycerol. Various samples of CuAl catalysts were prepared by co-precipitation at Cu: Al molar ratio 1:1 and were calcined at different temperatures (300–1000 °C). The obtained catalysts were reduced at 200 °C before their activity testing for glycerol hydrogenolysis reaction. To correlate the structure-activity, the catalysts were thoroughly characterized by XRD, XPS, BET, TEM, H2-TPR, NH3-TPD, and pyridine FTIR. It was observed that with an increase in calcination temperature from 300 to 700 °C, the glycerol conversion also increased from 47 to 55% with 93% selectivity to 1,2-PDO. The better performance of these catalysts was mainly related to the predominant presence of Brønsted acid sites, an appropriate ratio of the Cu0 to CuAl2O4 + CuO (0.33) and CuAl2O4 to CuO phases (0.35), the existence of Cu2O phase and the smaller Cu0 particle size. It was shown that altering the ramping rate for the calcination temperature of 400 °C impacted the catalytic activity. The CuAl-400 (DC) (direct calcined) catalyst exhibited a maximum glycerol conversion of 60%.

1 aMane, Rasika1 aPotdar, Aparna1 aJeon, Yukwon1 aRode, Chandrashekhar uhttps://library.ncl.res.in/content/calcination-temperature-impacting-structure-and-activity-cual-catalyst-aqueous-glycerol