Disclosed are methods for preparing zingerone from ginger using alkaline solutions, as well as compositions obtained using these methods, and methods for using these compositions. Specifically disclosed are pharmaceutical compositions, and treatment methods employing zingerone in combination with other therapeutics such as gentamicin, vancomycin, and cefotaxime.

A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a C.sub.4 diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) purging a portion to prevent propane build-up and (6) recovering product diisopropyl alcohol.

A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a C.sub.4 diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) purging a portion to prevent propane build-up and (6) recovering product diisopropyl alcohol.

A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a propane diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) allowing propane to build-up to an amount sufficient to operate as a diluent and (6) recovering product diisopropyl alcohol.

A process for the production of diisopropyl ether from high purity propylene without the need of a propane-propylene fractionation column has been developed. The process involves (1) reacting a high purity propylene feedstock and water to produce isopropyl alcohol in a reactor and reacting the isopropyl alcohol with propylene to produce diisopropyl ether in the presence of an acidic ion exchange resin catalyst and a propane diluent to generate a reactor effluent stream containing at least water, isopropyl alcohol, diisopropyl ether, propylene, and acid, (2) passing the reactor effluent to an acid removal zone to produce an acid-depleted stream, (3) dividing the acid-depleted stream into two portions, (4) recycling a portion to the reactor (5) allowing propane to build-up to an amount sufficient to operate as a diluent and (6) recovering product diisopropyl alcohol.

The invention relates to a two-stage method for recovering halogenated hydrocarbons. In a desorption step, steam is passed through an adsorbent comprising adsorbed halogenated hydrocarbons, which produces a secondary flow volume containing halogenated hydrocarbons. The secondary flow volume is converted into a condensate containing halogenated hydrocarbons and water by cooling, from which condensate the halogenated hydrocarbons are separated. In a sterilisation step that precedes the desorption step, the adsorbent comprising adsorbed halogenated hydrocarbons is brought into contact with steam for at least 10 minutes at a temperature of more than 120 C. and at a pressure between 0.15 MPa and 0.4 MPa.

The invention relates to a two-stage method for recovering halogenated hydrocarbons. In a desorption step, steam is passed through an adsorbent comprising adsorbed halogenated hydrocarbons, which produces a secondary flow volume containing halogenated hydrocarbons. The secondary flow volume is converted into a condensate containing halogenated hydrocarbons and water by cooling, from which condensate the halogenated hydrocarbons are separated. In a sterilisation step that precedes the desorption step, the adsorbent comprising adsorbed halogenated hydrocarbons is brought into contact with steam for at least 10 minutes at a temperature of more than 120 C. and at a pressure between 0.15 MPa and 0.4 MPa.

A process for separating at least one inositol from a carob extract, may include: chromatographically separating pinitol a first carob extract in at least one passage on a chromatographic resin, thus obtaining an aqueous solution comprising the pinitol in a range of from 35 to 70 wt. 8, based on a total aqueous solution weight, the aqueous solution having a Brix value of 20 or lower. The first carob extract may be filtered and demineralized carob extract having a Brix value greater than 60 and comprising the pinitol in a range of 5 to 25 wt. %, based on a total first carob extract weight.

A process for separating at least one inositol from a carob extract, may include: chromatographically separating pinitol a first carob extract in at least one passage on a chromatographic resin, thus obtaining an aqueous solution comprising the pinitol in a range of from 35 to 70 wt. 8, based on a total aqueous solution weight, the aqueous solution having a Brix value of 20 or lower. The first carob extract may be filtered and demineralized carob extract having a Brix value greater than 60 and comprising the pinitol in a range of 5 to 25 wt. %, based on a total first carob extract weight.

A process for separating at least one inositol from a carob extract, may include: chromatographically separating pinitol a first carob extract in at least one passage on a chromatographic resin, thus obtaining an aqueous solution comprising the pinitol in a range of from 35 to 70 wt. 8, based on a total aqueous solution weight, the aqueous solution having a Brix value of 20 or lower. The first carob extract may be filtered and demineralized carob extract having a Brix value greater than 60 and comprising the pinitol in a range of 5 to 25 wt. %, based on a total first carob extract weight.