The present invention provides a precursor film for producing a conductive film, the precursor film including: a substrate; a primer layer disposed on the substrate; and a plated layer precursor layer disposed on the primer layer, in which the plated layer precursor layer includes a bifunctional radical-polymerizable monomer and a polymer having a functional group which interacts with a plating catalyst or a precursor of the plating catalyst, and the bifunctional radical-polymerizable monomer has 25 to 100 atoms in a main chain of a linking chain which links two radical-polymerizable groups.

The invention relates to a commercially viable, cost effective and energy efficient process for the preparation of 2-(1H-Imidazol-4-yl)ethanamine or pharmaceutically acceptable salts thereof in high purity and yield via application of continuous flow technology.

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m.sup.3 to about 150 kg/m.sup.3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 m to about 150 m; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m.sup.2/g to about 300 m.sup.2/g and a geometric surface area per packed bed volume from about 550 m.sup.2/m.sup.3 to about 1500 m.sup.2/m.sup.3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.

The disclosure provides methods for the production of liquefied petroleum gas from sustainable feedstocks, including methods comprising conversion of alcohols produced by gas fermentation for the production of propane and/or butane.

The present invention relates to a method for producing a microfluidic device, in particular, a sol-gel method for producing a microfluidic device in hybrid silica glass. The invention also relates to a microfluidic device obtainable by the method as described above and to microfluidic device in hybrid silica glass comprising at least one microchannel having a depth of at least 1 m, preferably between 1 m and 1 mm, and more preferably between 10 and 100 m.

An RMA crosslinkable composition having at least one crosslinkable component including reactive components A and B each including at least 2 reactive groups, the at least 2 reactive groups of component A being acidic protons (CH) in activated methylene or methine groups and the at least 2 reactive groups of component B are activated unsaturated groups (CC) and a base catalyst (C) which reactive components A and B crosslink by Real Michael Addition (RMA) reaction under action of the base catalyst, characterised in that the at least one crosslinkable component including reactive components A and B in the composition have a total hydroxy number of less than 60, preferably less than 40 and more preferably less than 20 mg KOH/g solids. Further, specific resins A and B having a low hydroxy number for use in RMA cross-linkable compositions and a process for the manufacture thereof.

The invention relates to a commercially viable, cost effective and energy efficient process for the preparation of 2-(1H-Imidazol-4-yl)ethanamine or pharmaceutically acceptable salts thereof in high purity and yield via application of continuous flow technology.

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m.sup.3 to about 150 kg/m.sup.3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 m to about 150 m; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m.sup.2/g to about 300 m.sup.2/g and a geometric surface area per packed bed volume from about 550 m.sup.2/m.sup.3 to about 1500 m.sup.2/m.sup.3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.

A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a non-cyclic amide or thioamide based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the non-cyclic amide or thioamide based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation.

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m.sup.3 to about 150 kg/m.sup.3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 m to about 150 m; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m.sup.2/g to about 300 m.sup.2/g and a geometric surface area per packed bed volume from about 550 m.sup.2/m.sup.3 to about 1500 m.sup.2/m.sup.3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.