A method for synthesizing functionalized bio-based crosslinkers including forming a first mixture by mixing a bio-based carboxylic acid with an alkaline solution and forming a second mixture containing a functionalized bio-based crosslinker by reacting the bio-based carboxylic acid with a modifier. The modifier includes at least one of an epoxide group and an acrylate group. Reacting the bio-based carboxylic acid with the modifier includes forming a reaction mixture by mixing the first mixture with the modifier and exposing the reaction mixture to at least one of heating, ultrasound radiation, and microwave radiation.

The present invention relates to a method for preparing a glycidyl ester compound which comprises performing a reaction under reduced pressure without using a reaction solvent.

The present invention is directed to a process for the preparation of a hydrazine derivative by reaction of the corresponding oxirane with hydrazine, that uses as only solvent toluene. The process provides excellent yields and purities and allows to proceed without purification in a one-pot scheme. Toluene additionally reduces the excess of hydrazine needed to complete the reaction, significantly reducing the waste treatment costs and even allows the hydrazine to be recycled into the reaction.

The present invention is directed to a process for the preparation of a hydrazine derivative by reaction of the corresponding oxirane with hydrazine, that uses as only solvent toluene. The process provides excellent yields and purities and allows to proceed without purification in a one-pot scheme. Toluene additionally reduces the excess of hydrazine needed to complete the reaction, significantly reducing the waste treatment costs and even allows the hydrazine to be recycled into the reaction.

A continuous process for the preparation of propylene oxide, comprising a start-up stage and normal run stage, wherein the normal run stage comprises (i) continuously providing a liquid feed stream comprising propene, hydrogen peroxide, acetonitrile, a formate salt, water and optionally propane, wherein in the liquid feed stream, the molar amount of the formate salt relative to the molar amount of hydrogen peroxide at a given point of time during the normal run stage is a.sup.N(Fo/H.sub.2O.sub.2); (ii) continuously passing the liquid feed stream provided in (i) into an epoxidation zone comprising a catalyst comprising a titanium zeolite having framework type MWW, and subjecting the liquid feed stream to epoxidation reaction conditions in the epoxidation zone, obtaining a reaction mixture comprising propylene oxide, acetonitrile, water, the formate salt, optionally propene, and optionally propane; (iii) continuously removing an effluent stream from the epoxidation zone, the effluent stream comprising propylene oxide, acetonitrile, water, at least a portion of the formate salt, optionally propene, and optionally propane; wherein the normal run stage is characterized in an average rate of change of a.sup.N(Fo/H.sub.2O.sub.2) of less than 0 h.sup.1.

A continuous process for the preparation of propylene oxide, comprising a start-up stage and normal run stage, wherein the normal run stage comprises (i) continuously providing a liquid feed stream comprising propene, hydrogen peroxide, acetonitrile, a formate salt, water and optionally propane, wherein in the liquid feed stream, the molar amount of the formate salt relative to the molar amount of hydrogen peroxide at a given point of time during the normal run stage is a.sup.N(Fo/H.sub.2O.sub.2); (ii) continuously passing the liquid feed stream provided in (i) into an epoxidation zone comprising a catalyst comprising a titanium zeolite having framework type MWW, and subjecting the liquid feed stream to epoxidation reaction conditions in the epoxidation zone, obtaining a reaction mixture comprising propylene oxide, acetonitrile, water, the formate salt, optionally propene, and optionally propane; (iii) continuously removing an effluent stream from the epoxidation zone, the effluent stream comprising propylene oxide, acetonitrile, water, at least a portion of the formate salt, optionally propene, and optionally propane; wherein the normal run stage is characterized in an average rate of change of a.sup.N(Fo/H.sub.2O.sub.2) of less than 0 h.sup.1.

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20 C. to 50 C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60 C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20 C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20 C. to 50 C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60 C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20 C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.

Disclosed is a propylene direct oxidation reaction catalyst capable of preparing a propylene oxide from propylene and oxygen at a higher yield than catalysts prepared by conventional methods, by applying a specific transition metal oxide promoter in preparation of a catalyst containing silver, a transition metal oxide promoter and a carrier through a slurry process. The present invention provides a propylene direct oxidation reaction catalyst, which is a supported silver catalyst used for preparing a propylene oxide from the propylene direct oxidation reaction, the catalyst including a molybdenum oxide and a tungsten oxide as a catalyst promoter.

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20 C. to 50 C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60 C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20 C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.