Henkel Kommanditgesellschaft Auf Aktien

Theo Fleckenstein

Franz-Josef Carduck

Gerd Goebel

Joachim Pohl

Alexander Ditze

Thomas Hahn

Franz Kresse

Guenther Demmering

Franz J Carduck

Lutz Jeromin

Wilhelm Johannisbauer

Bernd-Dieter Holdt

Hans-Peter Kubersky

Norbert Bremus

Udo Kreutzer

Georg Fieg

Jurgen Falbe

Juergen Falbe

Reinhard Eicher

Gerd Geobel

Carpet cleaning formulation

Scatterable carpet cleaning formulation containing rollable particles

Scatterable carpet cleaning formulations

Hydrogenation process

Process for the catalytic hydrogenation of liquid fatty acid methyl

In the catalytic hydrogenation of fatty acid methyl esters, the fatty acid methyl esters are continuously reacted with hydrogen under pressures of from 20 to 100 bar and at temperatures of from 160.degree. to 270.degree. C. with molar ratios of hydrogen to fatty acid methyl ester substrate of from 10:1 to 500:1. The reaction is carried out over catalysts which contain from 30 to 40% by weight copper, from 23 to 30% by weight chromium, from 1 to 10% by weight manganese, from 1 to 10% by weight silicon and from 1 to 7% by weight barium (% by weight, based in each case on oxidic catalyst mass) and, if desired, other transition metals in the form of their oxides. After calcination of the components, the catalyst is converted into shaped particulate and/or granulated elements with from 1 to 10% by weight, based on oxidic catalyst, of at least one binder in addition to 1 to 10% by weight graphite. The catalyst is activated with hydrogen or a hydrogen-containing gas mixture. This process enables production of fatty alcohols in high yield from pre-separated distillation cuts of fatty acid methyl esters at low pressures and very low hydrocarbon formation.

Process for the hydrogenation of fatty acid methyl esters

A process for the separation of propylene glycol from a mixture of low-boiling fatty alcohols and propylene glycol which comprises extracting the mixture with water to produce a water-propylene glycol mixture and fractionating the water-propylene glycol mixture to produce propylene glycol that is substantially anhydrous and an apparatus for carrying out the process.

Process for the separation of propylene glycol from fatty alcohols

In the catalytic hydrogenation of fatty acid methyl ester mixtures, the mixtures are continuously reacted with hydrogen under pressures of from 100 to 300 bar and at temperatures of from 160.degree. to 270.degree. C. with molar ratios or hydrogen to fatty acid methyl ester mixture of from 10:1 to 500:1. The reaction is carried out over catalysts which contain from 30 to 40% by weight copper, from 23 to 30% by weight chromium, from 1 to 10% by weight manganese, from 1 to 10% by weight silicon and from 1 to 7% by weight barium (% by weight, based in each case on total weight of the oxidic catalyst) and, if desired, other transition metals in the form of their oxides. After calcination of the components, the catalyst is converted into shaped particulate and/or granulated elements with from 1 to 10% by weight, based on oxidic catalyst, of at least one binder in addition to 1 to 10% by weight graphite. The catalyst is activated with hydrogen or a hydrogen-containing gas mixture. This process enables production of fatty alcohols in high yield from fatty acid methyl ester mixtures containing fatty acid residues in the C.sub.8 to C.sub.22 carbon chain range without prior separation of the mixtures into individual boiling fractions.

Process for the hydrogenation of fatty acid methyl ester mixtures

In the direct catalytic hydrogenation of glyceride oils, the glyceride oils are continuously reacted with hydrogen under pressures of from 20 to 300 bar and at temperatures of from 160.degree. to 250.degree. C. with molar ratios of hydrogen to fatty acid residues in the glyceride oil substrate of from 10:1 to 500:1, the reaction being carried out over catalysts which contain from 30 to 40% by weight copper, from 23 to 30% by weight chromium, from 1 to 7% by weight barium (% by weight, based in each case on oxidic catalyst mass) and, if desired, other transition metals in the form of their oxides and which, after calcination of the components forming the catalyst mass, are converted into shaped particulate and/or granulated elements with from 1 to 10% by weight, based on oxidic catalyst, of at least one binder, and which have been activated with hydrogen or a hydrogen-containing gas mixture.

Process for direct hydrogenation of glyceride oils

A process for the catalytic hydrogenation of butterfat where non-deacidified butterfat is continuously reacted with hydrogen under pressures of from 20 to 300 bar and at temperatures of from 180.degree. to 250.degree. C. with molar ratios of hydrogen to fatty acid residue in the butterfat of from 10:1 to 500:1. The reaction is carried out over catalysts which contain from 30 to 40% by weight copper, from 23 to 30% by weight chromium, from 1 to 10% by weight manganese, from 1 to 10% by weight silicon, and from 1 to 7% by weight barium. The percentages by weight in each case are based on the total oxidic mass of the catalyst. Other transition metals, especially zirconium and cerium, are additionally incorporated into the catalyst. The metals in the catalyst are converted to their oxides by calcination. The catalyst is converted into shaped particulate or granulated elements with from 1 to 10% by weight of at least one binder in addition to 1 to 10% by weight graphite. The catalyst is activated with hydrogen or a hydrogen-containing gas mixture. The reaction products include alcohols, oxo- and hydroxyfatty alcohols corresponding to the natural fatty acid composition of the butterfat and the desired, valuable product, propylene glycol. This process is advantageous since it eliminates the need for preseparation of the relatively short-chain fatty acids (or deacidification) of the butterfat prior to hydrogenation.

Process for the direct hydrogenation of butterfat

A process for the catalytic hydrogenation of liquid fatty acid triglycerides and the simultaneous recovery of fatty alcohols and C.sub.3 diols in the presence of gaseous hydrogen and hydrogenation catalysts under pressures of from 50 to 300 bar and at temperatures in the range from 160.degree. to 250.degree. C., to produce fatty alcohols in at least 99% of the theoretical yield and of 1,2-propanediol in at least 80% of the theoretical yield and a maximum paraffin content of 0.5% of the theoretical yield is disclosed. The hydrogenation reaction is carried out in a tube bundle reactor operated under isothermal conditions through a cooling or heating fluid, the liquid phase being passed as co-current trickle phase with the gaseous phase over catalyst packings in the individual reactor tubes without back-mixing, and in that the load per unit volume of the reactor is selected between 0.2 and 2.5 l starting material per 1 reactor volume per hour and the load per unit area of each individual reactor tube between 1.5 and 25 m.sup.3 starting material per m.sup.2 reactor cross-section per hour and the reaction parameters of temperature and pressure are adapted in accordance with the actual catalyst activity.

Process for producing fatty alcohols and C.sub.3 diols by catalytic

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Hilden, Germany

Theo Fleckenstein