Hydrotreatment of nonedible jatropha oils over PtPd/Al 2 O 3 catalyst and NiMoP/Al 2 O 3 catalysts was investigated under conditions of 330−390 °C, 3 MPa and 2 h −1 in a fixed-bed reactor. A significantly high yield range of about 82 wt % of liquid hydrocarbon products was achieved over all catalysts. Moreover, the liquid hydrocarbon products have low acid number, suitable density and viscosity, and quite high cetane index. The oil can be a high-performance additive for diesel oil. The oxygen removal pathway of jatropha oil over PtPd/Al 2 O 3 catalyst is primarily compiled through decarboxylation and/or decarbonylation, but over NiMoP/Al 2 O 3 catalysts, the oxygen removal pathways are executed primarily by hydro-deoxygenation. A long-term experiment was conducted over catalyst A (NiMoP/Al 2 O 3 ). Results show that catalyst A starts deactivation from reaction time of 120 h. The sulfide catalyst conversion to oxide catalyst is regarded as the main reason for deactivation. The deactivated catalyst can be reused after regeneration treatment.
A method for forming organic single-crystal arrays from solution is demonstrated using an organic semiconductor, 3,9-bis(4-ethylphenyl)-peri-xanthenoxanthene (C(2) Ph-PXX). Supersaturation of C(2) Ph-PXX/tetralin solution is spatially changed by making a large difference in solvent evaporation to generate nuclei at the designated location. The method is simple to implement since it employs only a micropattern and control of the solvent vapor pressure during growth.
Hydrotreatment of jatropha oil over a series of sulfided NiMo/SiO 2 -Al 2 O 3 and NiMo/ZSM-5-Al 2 O 3 catalysts using a fixed-bed reactor was carried out. Effect of support on various reactions occurring in hydrotreatment was investigated. For NiMo/SiO 2 -Al 2 O 3 series catalysts, the rates of decarboxylation and/or decarbonylation increased with increasing Si/(Si+Al) ratio, while the ratio of hydrodeoxygenation decreased with increasing Si/(Si+Al) ratio. For NiMo/ZSM-5-Al 2 O 3 series catalysts, with increasing addition amount of ZSM-5, the rate of decarboxylation and/or decarbonylation versus hydrodeoxygenation did not change. These results could be attributed to that the total acidic sites of catalyst could have a positive effect on the decarboxylation and/or decarbonylation pathways.NiMo/SiO 2 -Al 2 O 3 catalysts showed much higher isomerization/cracking ratio than NiMo/ZSM-5-Al 2 O 3 catalysts. It was suggested that isomerization reaction was favorable for weak and middle acidic site but cracking reaction was favorable for strong acidic site.
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