A method includes: providing a mixture including at least one alkyl tosylate and a Grignard reagent; and reacting the at least one alkyl tosylate with the Grignard reagent in a C—C coupling reaction mechanism to form a branched aliphatic alcohol.

The present invention relates to synthetic membranes and use of these synthetic membranes for isolation of volatile organic compounds and purification of water. The synthetic membrane includes a hydrophobic polymer layer located on a polymeric membrane support layer. The invention includes a method of isolating volatile organic compounds with the synthetic membrane by contacting a volatile organic mixture with the hydrophobic polymer layer of the synthetic membrane and removing volatile organic compounds from the polymeric membrane support layer of the synthetic membrane by a process of pervaporation. The invention also includes a method of purifying water with the synthetic membrane by contacting an ionic solution with the hydrophobic polymer layer of the synthetic membrane and removing water from the polymeric membrane support layer of the synthetic membrane by a process of reverse osmosis. The invention also relates to methods of isolating non-polar gases by gas fractionation.

An approach is provided for processing mixed solid waste using an integrated bioenergy complex. The approach, for instance, involves receiving the mixed solid waste at the integrated bioenergy complex, the integrated bioenergy complex including an organic conversion processing center and an inorganic conversion processing center. The approach also involves separating the mixed solid waste into recyclables, an organic waste stream, and an inorganic waste stream. The approach further involves feeding the organic waste stream to the organic conversion processing center to produce organic conversion products and an organic residual, and feeding the organic residual and the inorganic waste stream to the inorganic conversion processing center to produce inorganic conversion products, electric power, and a residual waste. The electric power is used to partially or fully power the organic conversion processing center, and residual waste is less than a target percentage of the received mixed solid waste.

An approach is provided for processing mixed solid waste using an integrated bioenergy complex. The approach, for instance, involves receiving the mixed solid waste at the integrated bioenergy complex, the integrated bioenergy complex including an organic conversion processing center and an inorganic conversion processing center. The approach also involves separating the mixed solid waste into recyclables, an organic waste stream, and an inorganic waste stream. The approach further involves feeding the organic waste stream to the organic conversion processing center to produce organic conversion products and an organic residual, and feeding the organic residual and the inorganic waste stream to the inorganic conversion processing center to produce inorganic conversion products, electric power, and a residual waste. The electric power is used to partially or fully power the organic conversion processing center, and residual waste is less than a target percentage of the received mixed solid waste.

An approach is provided for processing mixed solid waste using an integrated bioenergy complex. The approach, for instance, involves receiving the mixed solid waste at the integrated bioenergy complex, the integrated bioenergy complex including an organic conversion processing center and an inorganic conversion processing center. The approach also involves separating the mixed solid waste into recyclables, an organic waste stream, and an inorganic waste stream. The approach further involves feeding the organic waste stream to the organic conversion processing center to produce organic conversion products and an organic residual, and feeding the organic residual and the inorganic waste stream to the inorganic conversion processing center to produce inorganic conversion products, electric power, and a residual waste. The electric power is used to partially or fully power the organic conversion processing center, and residual waste is less than a target percentage of the received mixed solid waste.

Catalyst compositions for the conversion of aldehyde compounds and primary alcohol compounds to olefins are disclosed herein. Reactions include oxidative dehydroxymethylation processes and oxidative dehydroformylation methods, which are beneficially conducted in the presence of a sacrificial acceptor of H.sub.2 gas, such as N,N-dimethylacrylamide.

Catalyst compositions for the conversion of aldehyde compounds and primary alcohol compounds to olefins are disclosed herein. Reactions include oxidative dehydroxymethylation processes and oxidative dehydroformylation methods, which are beneficially conducted in the presence of a sacrificial acceptor of H.sub.2 gas, such as N,N-dimethylacrylamide.

An ionic liquid as a solvent in the hydration reaction of α-pinene to α-terpineol. The ionic liquid is obtained from the reaction of an amine and an inorganic acid. The use of the ionic liquid as solvent favors the selectivity towards the formation of α-terpineol and once the reaction product has been brought to room temperature, the organic phase can be physically separated from the inorganic one by decantation. The inorganic phase contains the ionic liquid, water and reaction catalyst and can be directly reused for a new reaction batch.

An ionic liquid as a solvent in the hydration reaction of α-pinene to α-terpineol. The ionic liquid is obtained from the reaction of an amine and an inorganic acid. The use of the ionic liquid as solvent favors the selectivity towards the formation of α-terpineol and once the reaction product has been brought to room temperature, the organic phase can be physically separated from the inorganic one by decantation. The inorganic phase contains the ionic liquid, water and reaction catalyst and can be directly reused for a new reaction batch.

A process for preparing C.sub.4 to C.sub.13 monohydroxy compounds from a bottom fraction arising in the distillation of a crude mixture of C.sub.4 to C.sub.13 oxo-process aldehydes from cobalt-catalyzed or rhodium-catalyzed hydroformylation, or in the distillation of a crude mixture of C.sub.4 to C.sub.13 oxo-process alcohols, which comprises contacting the bottom fraction in the presence of hydrogen with a catalyst comprising copper oxide and aluminum oxide, at a temperature of 150° C. to 300° C. and a pressure of 20 bar to 300 bar and subjecting the resulting crude hydrogenation product to distillation, and the amount of C.sub.4 to C.sub.13 monohydroxy compounds present in the crude hydrogenation product after the hydrogenation being greater than the amount of C.sub.4 to C.sub.13 monohydroxy compounds given stoichiometrically from the hydrogenation of the ester and aldehyde compounds present in the bottom fraction, including the C.sub.4 to C.sub.13 monohydroxy compounds still present in the bottom fraction before the hydrogenation.