Continuous-Flow Production of Isosorbide from Aqueous-Cellulosic Derivable Feed over Sustainable Heterogeneous Catalysts

Abstract

Continuous-flow sorbitol dehydration in liquid water was performed on β zeolite (Si/Al molar ratio = 75) with conversion of 94 and 83 mol % isosorbide yield. This efficiency is due to the three-dimension pore architecture, high specific surface area (520 m2 g–1), and Brønsted acid sites of 69 μmol g–1. The pore size of β zeolite (6.6 × 6.7 Å2) is slightly larger than the cross section of sorbitol and isosorbide and enables an efficient diffusion of the reactant and product to/from the pores. Operation in continuous flow allows rapid dehydration of sorbitol to 1,4-sorbitan, after which the latter got converted to isosorbide. The high yield of isosorbide is attributed to the continuous removal of the formed products from the catalyst surface. Finally, direct isosorbide production from aqueous glucose solution via hydrogenation on Ni catalyst supported on nitrogen-doped carbon, followed by dehydration of the formed sorbitol to isosorbide, was pioneered.

A Cooperative OSDA Blueprint for Highly Siliceous Faujasite Zeolite Catalysts with Enhanced Acidity Accessibility

“…Then on-detected Al in pyridine-IR measurements should mainly correspond to those Al contents in sod cage or to weak acid Al species. [46][47][48] These results explicitly confirm that unique Al distributions have been obtained in the high-silica FAUz eolites prepared via the presented cooperative OSDAs trategy,w hich has never been reported before in literature regarding high-silica FAUz eolites.…”

“…[30,33] FAU-S1 and FAU-S2 were selected because of their pure FAUphase obtained with high seeds loading (10 %) at different temperatures (110 8 8Ca nd 120 8 8C, respectively);h ighly siliceous FAU-S3 and FAU-S4 were chosen because of their minute seed usage (1 %), which would not significantly change the overall gel composition, but translates to ahigher seeding efficiencyand apotentially lower manufacturing cost as indicated by the solid product yields (Table S2, entries 26-29, entries 39-42). In consideration of the gel composition differences between the highsilica FAUa nd the two benchmark samples (e.g.N a + ,H 2 O, seeds amount), another six benchmark recipes were carried out with similar synthesis compositions of FAU-S4 but using CE or Ch + as the only OSDA( so digressing from reported "CE or Ch + only" recipes in literature) (Table S2, entries [46][47][48][49][50][51]. Themajority product in all these benchmark recipes was never FAU( Figures S8,S9).…”

Controlled lignosulfonate depolymerizationviasolvothermal fragmentation coupled with catalytic hydrogenolysis/hydrogenation in a continuous flow reactor

“…68 The XRD diffraction patterns of the spent catalyst after 9 h of TOS (35Ni/NDC-TOS) showed similar peaks to the spent catalyst after 1 h (Figure S22 One of the advantages of operating in continuous flow systems is the possibility to couple multiple reactors together. 67 Herein, two identical packed reactors with 35Ni/NDC have been coupled in series, in order to prolong the contact time between the LS solution and the catalyst and consequently optimize the monomer yield (Figure 6 and Figure S5 in ESI). Moreover, coupling two flow reactors in series aims to mimic an industrial scale up of such process.…”

“…64,65 All these studies were performed in batch systems, which presents disadvantages when compared to continuous flow systems, e.g., complex product-catalyst separation, time, energy-consumption in discontinuous steps and cost efficiency . 10,12,59,66,67 Horáček et al 52 only reported the LS fragmentation in a continuous flow system at a high reaction temperature (320°C) over bimetallic Ni and Mo catalyst supported on Al 2 O 3 . In this study and due to over hydrogenation, guaiacol was found the major product of LS catalytic fragmentation (yield higher than 1.8 wt.-%).…”

A sustainable approach to cathode delamination using a green solvent

“…33 At present, isosorbide production has attracted widespread attention and is anticipated to reach US $324.6 million in the next few years. 34,35 Several facile synthetic strategies for DMI have been reported 33,36,37 to increase its availability at a cheaper price. The close proximity of the Hildebrand solubility parameters (d T ) of DMI to PVDF suggests its suitability as a dissolution solvent.…”