Abstract: 3,3-Dimethylbutanal is prepared from 3,3-dimethybutanol. Intermediate 3,3-dimethylbutanol is obtained by reacting ethylene, isopropylene and a mineral acid to produce a 3,3-dimethylbutyl ester which is hydrolyzed to the alcohol. The hydrolysis step is effectively carried out by reactive distillation. Alternatively, 3,3-dimethylbutanal is prepared from 3,3-dimethylbutanol obtained by reduction of the corresponding carboxylic acid or 1,2-epoxy-3,3-dimethylbutane, or by hydrolysis of 1-halo-3,3-dimethylbutane. Fixed bed gas phase and stirred tank liquid phase processes are provided for converted 3,3-dimethylbutanol to 3,3-dimethylbutanal by catalytic dehydrogenation.

Abstract: 3,3-Dimethylbutanal is prepared from 3,3-dimethylbutanol. Intermediate 3,3-dimethylbutanol is obtained by reacting ethylene, isopropylene and a mineral acid to produce a 3,3-dimethylbutyl ester which is hydrolyzed to the alcohol. The hydrolysis step is effectively carried out by reactive distillation. Alternatively, 3,3-dimethylbutanal is prepared from 3,3-dimethylbutanol obtained by reduction of the corresponding carboxylic acid or 1,2-epoxy-3,3-dimethylbutane, or by hydrolysis of 1-halo-3,3-dimethylbutane. Fixed bed gas phase and stirred tank liquid phase processes are provided for converting 3,3-dimethylbutanol to 3,3-dimethylbutanal by catalytic dehydrogenation.

Abstract: 3,3-Dimethylbutanal is prepared from 3,3-dimethylbutanol. Intermediate 3,3-dimethylbutanol is obtained by reacting ethylene, isopropylene and a mineral acid to produce a 3,3-dimethylbutyl ester which is hydrolyzed to the alcohol. The hydrolysis step is effectively carried out by reactive distillation. Alternatively, 3,3-dimethylbutanal is prepared from 3,3-dimethylbutanol obtained by reduction of the corresponding carboxylic acid or 1,2-epoxy-3,3-dimethylbutane, or by hydrolysis of 1-halo-3,3-dimethylbutane. Fixed bed gas phase and stirred tank liquid phase processes are provided for converting 3,3-dimethylbutanol to 3,3-dimethylbutanal by catalytic dehydrogenation.

Abstract: 3,3-Dimethylbutanal is prepared from 3,3-dimethylbutanol. Intermediate 3,3-dimethylbutanol is obtained by reacting ethylene, isopropylene and sulfuric acid to produce a 3,3-dimethylbutyl ester which is hydrolyzed to the alcohol. The hvdrolysis step is effectively carried out by reactive distillation. Alternatively, 3,3-dimethylbutanal is prepared from 3,3-dimethylbutanol obtained by reduction of the corresponding carboxylic acid or 1,2-epoxy-3,3-dimethylbutane, or by hydrolysis of 1-halo-3,3-dimethylbutane. Fixed bed gas phase and stirred tank liquid phase processes are provided for converting 3,3-dimethylbutanol to 3,3-dimethylbutanal by catalytic dehydrogenation.

Abstract: Polyhydroxyalkanoate (PHA) polyester is extracted from biomass by dissolving the PHA in a non-halogenated solvent which comprises a PHA-poor solvent that dissolves less than 1% of the PHA at temperatures less than the solvent boiling point, or a mixture of a PHA-poor solvent and a PHA-good solvent. Following extraction of PHA under pressure at a temperature above about 80.degree. C., typically above the boiling point of the PHA-poor solvent, PHA polymer is precipitated by cooling the PHA-enriched solvent mixture. Suitable PHA-poor solvents can include linear and branched R.sub.1 --OH alcohols and R.sub.2 --COOR.sub.3 esters where R.sub.1 =C.sub.1 -C.sub.4, R.sub.2 =H, C.sub.1,C.sub.2, or C.sub.3, and R.sub.3 =C.sub.1 -C.sub.5.

Abstract: Polyhydroxyalkanoate (PHA) polyester is extracted from biomass by dissolving the PHA in a non-halogenated solvent which comprises a PHA-good solvent or a mixture thereof. Suitable PHA-good solvents can be selected from the disclosed alcohols, esters, amides and ketones. The PHA can be recovered, for example, by cooling, by solvent evaporation, or by addition of a PHA-poor solvent, wherein the PHA-poor solvent preferably dissolves less than about 1% (w/v) of the PHA at a temperature below the solvent boiling point. Preferred PHA types for use in the invention are poly (hydroxybutyrate-co-hydroxyvalerate), poly(3-hydroxybutyrate-co-4-hydroxybutyrate), and polymers/copolymers of hydroxyterminated polyhydroxybutyrate.

Abstract: A process for preparing isocyanates comprising contacting carbon dioxide and a primary amine in the presence of an aprotic organic solvent and a base selected from the group consisting of a phosphazene compound, an organic, nitrogenous base and mixtures thereof, wherein the organic, nitrogenous base selected from the group consisting of guanidine compounds, amidine compounds, tertiary amines and mixtures thereof to produce the corresponding ammonium carbamate salt, reacting the ammonium carbamate salt with an anhydride dehydrating agent to produce a product stream comprising the corresponding isocyanate, the aprotic organic solvent and the base salt derived from the anhydride, separating the base salt from the product stream, recovering and recycling the base, and regenerating and recycling the anhydride dehydrating agent.

Abstract: There is disclosed a continuous method for agglomerating lactices of a polymer to provide large particles. An acid anhydride solution is continuously admixed with an aqueous latex of a polymer followed by passing the admixture through a conduit with laminar-flow wherein the passage-time through said conduit is sufficient to hydrolyze the acid anhydride and produce agglomeration of said particles providing an agglomerated admixture followed by continuously stabilizing said agglomerated admixture with an emulsifying material providing a stabilized agglomerated latex.

Abstract: There is disclosed an apparatus for the continuous agglomeration of aqueous latices to provide large particles comprising a mixing zone for forming an admixture of an agglomerating solution and a latex having mixing means and a perforated member as one wall section providing a flowthrough port for the admixture inducing laminar-flow in the admixture, an annular conduit to carry the admixture during agglomeration, a low-shear zone to carry and stabilize the agglomerated admixture and a withdrawal means having at least one diameter reduction to flow-mix the stabilized agglomerated admixture during withdrawal.