Method for preparing methyl formate and coproducing dimethyl ether by reacting a formaldehyde and methanol raw material (molar ratio range of 1:4 to 1:0.05) in a First Reaction Region at ranges from 50 C. to 100 C. with Catalyst A resulting in post-reaction material separated into Constituent I. Reacting Constituent I in a Second Reaction Region at ranges from 50 C. to 200 C. and from 0.1 MPa to 10 MPa with Catalyst B resulting in post-reaction material, which is separated into methyl formate, dimethyl ether and Constituent II. At least 1% of dimethyl ether is product, and recycling the rest to the First Reaction Region. Constituent II is recycled to the Second Reaction Region. Each component is gaseous phase and/or liquid phase, independently. The method shows long catalyst life, mild reaction condition, high utilization ratio of raw materials, continuous production and large scale industrial application potential.

Disclosed herein is a method of preparing a catalyst having PtPd dispersed in polymer electrolyte multilayers, suitable for use in production of hydrogen peroxide, wherein the use of the catalyst prepared by forming polymer electrolyte multilayers on an anionic resin support and performing sulfuric acid treatment and loading (insertion or attachment) of PtPd particles can result in high hydrogen conversion, hydrogen selectivity and hydrogen peroxide yield for a long period of time.

Disclosed herein is a method of preparing a catalyst having PtPd dispersed in polymer electrolyte multilayers, suitable for use in production of hydrogen peroxide, wherein the use of the catalyst prepared by forming polymer electrolyte multilayers on an anionic resin support and performing sulfuric acid treatment and loading (insertion or attachment) of PtPd particles can result in high hydrogen conversion, hydrogen selectivity and hydrogen peroxide yield for a long period of time.

Disclosed is a process for preparing at least one ether compound, comprising reacting at least one alcohol (I) with at least one polyol (II) in the presence of a functional polymer [polymer (F)] as a catalyst (X), wherein: the alcohol (I) is represented by the general formula (1): R1-OH (1) wherein R1 is a hydrocarbon group having 1 to 36 carbon atoms, the polyol (II) is represented by the general formula (2): R2-(OH) m (2) wherein R2 represents the skeleton moiety of the polyol and m is an integer of from 2 to 20, and polymer (F) is a polymer comprising recurring units derived from at least one ethylenically unsaturated monomer [monomer (M)] and bearing at least one cation exchange group. Further disclosed is a surfactant composition obtained by said process, and featuring an excellent detergency performance.

Disclosed is a process for preparing at least one ether compound, comprising reacting at least one alcohol (I) with at least one polyol (II) in the presence of a functional polymer [polymer (F)] as a catalyst (X), wherein: the alcohol (I) is represented by the general formula (1): R1-OH (1) wherein R1 is a hydrocarbon group having 1 to 36 carbon atoms, the polyol (II) is represented by the general formula (2): R2-(OH) m (2) wherein R2 represents the skeleton moiety of the polyol and m is an integer of from 2 to 20, and polymer (F) is a polymer comprising recurring units derived from at least one ethylenically unsaturated monomer [monomer (M)] and bearing at least one cation exchange group. Further disclosed is a surfactant composition obtained by said process, and featuring an excellent detergency performance.

A method of making solid acid catalysts includes the step of sulfonating waste tire pieces in a first sulfonation step. The sulfonated waste tire pieces are pyrolyzed to produce carbon composite pieces having a pore size less than 10 nm. The carbon composite pieces are then ground to produce carbon composite powders having a size less than 50 m. The carbon composite particles are sulfonated in a second sulfonation step to produce sulfonated solid acid catalysts. A method of making biofuels and solid acid catalysts are also disclosed.

The present invention relates to the treatment of a promoted strong acid ion exchange resin for use as an acid catalyst with an antioxidant to protect the resin from oxidative degradation and the use of said treated promoted ion exchange resin catalyst in chemical production processes.

The present invention relates to the treatment of a promoted strong acid ion exchange resin for use as an acid catalyst with an antioxidant to protect the resin from oxidative degradation and the use of said treated promoted ion exchange resin catalyst in chemical production processes.

The invention relates to a process for the preparation of 1-(1,3-benzodioxol-5-yl)-1-propanone comprising the step of reacting 3,4-dimethylendioxybenzene with propionic anhydride in the presence of a bulk or supported catalyst, being said catalyst selected from the group of a sulphonated cross-linked divinylbenzene resin, a sulphonated cross-linked divinylbenzene resin partially exchanged with iron, zinc or gallium, a perfluorinated sulphonic resin, and a perfluorinated sulphonic resin partially exchanged with iron, zinc or gallium, wherein said catalyst has an average particle size from 1 m to 300 m, preferably from 1 m to 180 m, more preferably from 1 m to 100 m as measured with DLS (Dynamic light scattering) or a granulometer. The process is advantageously carried out at stoichiometric ratio between the reagents and with a continuous process.

The invention relates to a process for the preparation of 1-(1,3-benzodioxol-5-yl)-1-propanone comprising the step of reacting 3,4-dimethylendioxybenzene with propionic anhydride in the presence of a bulk or supported catalyst, being said catalyst selected from the group of a sulphonated cross-linked divinylbenzene resin, a sulphonated cross-linked divinylbenzene resin partially exchanged with iron, zinc or gallium, a perfluorinated sulphonic resin, and a perfluorinated sulphonic resin partially exchanged with iron, zinc or gallium, wherein said catalyst has an average particle size from 1 m to 300 m, preferably from 1 m to 180 m, more preferably from 1 m to 100 m as measured with DLS (Dynamic light scattering) or a granulometer. The process is advantageously carried out at stoichiometric ratio between the reagents and with a continuous process.