Methods and systems for preparing acetone from cumene hydroperoxide (CHP) are disclosed. The disclosed methods involve cleaving CHP to form a cleavage product stream. In some embodiments, the cleavage product stream is separated into an overhead stream and a bottoms stream. The bottoms stream is neutralized, washed and then treated in a crude acetone column to provide a crude acetone stream. The overhead stream of the cleavage product is flashed forward in the process, bypassing the neutralization, washing, and crude acetone column and is then combined with the crude acetone stream. The combined acetone streams are provided to an acetone product column. According to some embodiments, the acetone product column comprises a side draw for obtaining a recycle acetone stream, which is recycled to the cleavage reactor(s). The recycle acetone side draw may be located lower on the acetone product column than the point from which product acetone is obtained. The disclosed methods increase the efficiency of the process.

Methods and systems for preparing acetone from cumene hydroperoxide (CHP) are disclosed. The disclosed methods involve cleaving CHP to form a cleavage product stream. In some embodiments, the cleavage product stream is separated into an overhead stream and a bottoms stream. The bottoms stream is neutralized, washed and then treated in a crude acetone column to provide a crude acetone stream. The overhead stream of the cleavage product is flashed forward in the process, bypassing the neutralization, washing, and crude acetone column and is then combined with the crude acetone stream. The combined acetone streams are provided to an acetone product column. According to some embodiments, the acetone product column comprises a side draw for obtaining a recycle acetone stream, which is recycled to the cleavage reactor(s). The recycle acetone side draw may be located lower on the acetone product column than the point from which product acetone is obtained. The disclosed methods increase the efficiency of the process.

A coating composition including at least one solvent, at least one resin, at least one drier, and an anti-skinning agent is provided, an anti-skinning composition, wherein the anti-skinning composition comprises at least 92 wt. %, or more particularly at least 98 wt. %, of an alkyl oxime having five carbon atoms selected from 2-pentanone oxime and 3-methyl-2-butanone oxime. In some embodiments, the high-purity 2-pentanone oxime includes less than 0.5 wt. % methyl isobutyl ketoxime. In some embodiments, the composition includes less than 0.006 wt. % methyl isobutyl ketoxime. A method for the preparation of a purified 2-pentanone stream suitable for oximation to a high-purity 2-pentanone oxime is also provided.

A coating composition including at least one solvent, at least one resin, at least one drier, and an anti-skinning agent is provided, an anti-skinning composition, wherein the anti-skinning composition comprises at least 92 wt. %, or more particularly at least 98 wt. %, of an alkyl oxime having five carbon atoms selected from 2-pentanone oxime and 3-methyl-2-butanone oxime. In some embodiments, the high-purity 2-pentanone oxime includes less than 0.5 wt. % methyl isobutyl ketoxime. In some embodiments, the composition includes less than 0.006 wt. % methyl isobutyl ketoxime. A method for the preparation of a purified 2-pentanone stream suitable for oximation to a high-purity 2-pentanone oxime is also provided.

A coating composition including at least one solvent, at least one resin, at least one drier, and an anti-skinning agent is provided, an anti-skinning composition, wherein the anti-skinning composition comprises at least 92 wt. %, or more particularly at least 98 wt. %, of an alkyl oxime having five carbon atoms selected from 2-pentanone oxime and 3-methyl-2-butanone oxime. In some embodiments, the high-purity 2-pentanone oxime includes less than 0.5 wt. % methyl isobutyl ketoxime. In some embodiments, the composition includes less than 0.006 wt. % methyl isobutyl ketoxime. A method for the preparation of a purified 2-pentanone stream suitable for oximation to a high-purity 2-pentanone oxime is also provided.

A process can be used for preparing aldehydes from C2 to C20 olefins with a subsequent thermal separation for removal of the aldehyde formed. The process involves a membrane separation, which is preceded by performance of a gas exchange by which the proportion of the partial pressure represented by carbon monoxide or hydrogen is increased in order to reduce catalyst losses.

A process can be used for preparing aldehydes from C2 to C20 olefins with a subsequent thermal separation for removal of the aldehyde formed. The process involves a membrane separation, which is preceded by performance of a gas exchange by which the proportion of the partial pressure represented by carbon monoxide or hydrogen is increased in order to reduce catalyst losses.

A process for the production of normal-butanol, iso-butanol and 2-alkyl alkanol is disclosed. The process comprises: hydrogenating a feed comprising normal butyraldehyde, iso-butyraldehyde and 2-alkyl alkenal to form a crude product stream comprising normal-butanol, iso-butanol, 2-alkyl alkanol, unreacted normal butyraldehyde, unreacted iso-butyraldehyde and one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol; separating the crude product stream to produce: a mixed butanol stream having higher concentrations of normal butanol, iso-butanol, unreacted normal butyraldehyde and unreacted iso-butyraldehyde than the crude product stream; and a crude 2-alkyl alkanol stream having higher concentrations of 2-alkyl alkanol and the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol than the crude product stream; separating the mixed butanol stream to produce: a refined normal butanol stream having a higher concentration of normal butanol than the mixed butanol stream; and a crude iso-butanol stream having a higher concentration of iso-butanol than the mixed butanol stream; feeding the crude iso-butanol stream to a first polishing hydrogenation reactor wherein at least some of the unreacted iso-butyraldehyde is converted to iso-butanol to produce a polished iso-butanol stream; separating the polished iso-butanol stream to produce: a refined iso-butanol stream having a higher concentration of iso-butanol than the polished iso-butanol stream; and a light waste stream; separating the crude 2-alkyl alkanol stream to produce: an intermediate 2-alkyl alkanol stream having higher concentrations of 2-alkyl alkanol and the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol than the crude 2-alkyl alkanol stream; and a heavy waste stream; feeding the intermediate 2-alkyl alkanol stream to a second polishing hydrogenation reactor wherein at least some of the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol is converted to 2-alkyl alkanol to produce a polished 2-alkyl alkanol stream having a higher concentration of 2-alkyl alkanol than the intermediate 2-alkyl alkanol stream; separating the polished 2-alkyl alkanol stream to produce: a refined 2-alkyl alkanol stream having a higher concentration of 2-alkyl alkanol than the polished 2-alkyl alkanol stream; and an intermediate waste stream.

A process for the production of normal-butanol, iso-butanol and 2-alkyl alkanol is disclosed. The process comprises: hydrogenating a feed comprising normal butyraldehyde, iso-butyraldehyde and 2-alkyl alkenal to form a crude product stream comprising normal-butanol, iso-butanol, 2-alkyl alkanol, unreacted normal butyraldehyde, unreacted iso-butyraldehyde and one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol; separating the crude product stream to produce: a mixed butanol stream having higher concentrations of normal butanol, iso-butanol, unreacted normal butyraldehyde and unreacted iso-butyraldehyde than the crude product stream; and a crude 2-alkyl alkanol stream having higher concentrations of 2-alkyl alkanol and the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol than the crude product stream; separating the mixed butanol stream to produce: a refined normal butanol stream having a higher concentration of normal butanol than the mixed butanol stream; and a crude iso-butanol stream having a higher concentration of iso-butanol than the mixed butanol stream; feeding the crude iso-butanol stream to a first polishing hydrogenation reactor wherein at least some of the unreacted iso-butyraldehyde is converted to iso-butanol to produce a polished iso-butanol stream; separating the polished iso-butanol stream to produce: a refined iso-butanol stream having a higher concentration of iso-butanol than the polished iso-butanol stream; and a light waste stream; separating the crude 2-alkyl alkanol stream to produce: an intermediate 2-alkyl alkanol stream having higher concentrations of 2-alkyl alkanol and the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol than the crude 2-alkyl alkanol stream; and a heavy waste stream; feeding the intermediate 2-alkyl alkanol stream to a second polishing hydrogenation reactor wherein at least some of the one or more of unreacted 2-alkyl alkenal, 2-alkyl alkanal or 2-alkyl alkenol is converted to 2-alkyl alkanol to produce a polished 2-alkyl alkanol stream having a higher concentration of 2-alkyl alkanol than the intermediate 2-alkyl alkanol stream; separating the polished 2-alkyl alkanol stream to produce: a refined 2-alkyl alkanol stream having a higher concentration of 2-alkyl alkanol than the polished 2-alkyl alkanol stream; and an intermediate waste stream.

Methacrolein is prepared in a continuous process by a Mannich condensation reaction of formaldehyde with propanal. A methacrolein polymerization inhibitor is introduced during the production process and a part thereof is recycled back into the reactor where the Mannich condensation reaction is carried out.