Henkel Kommanditgesellschaft Auf Aktien

Cognis Deutschland Gmbh & Co. Kg

Eberhard Peukert

Lutz Jeromin

Bernhard Gutsche

Gerhard Wollmann

Klemens Eckwert

Bernard Schleper

Friedrich Hommers

Karl-Heinz Schmid

Alfred Meffert

Horst Rutzen

Wilhelm Johannisbauer

Frank Bongardt

Guenther Demmering

Lothar Friesenhagen

Wolfgang Schmidt

Gerhard Blasey

Guenter Panthel

Roland Hourticolon

Reinhold Sedelies

Udo Steinberner

Christoph Breucker

Levent Yueksel

Hans-Peter Kubersky

Udo Kreutzer

Karl-Heinz Buettgen

Juergen Latzel

Norbert Bremus

Gerhard Dieckelmann

Gerhard Mueller

Heinz Bollweg

Kurt Adrian

Hans-Guenther Richard

Hermann Frankenbach

Naturally occurring fats, oils and fatty derivatives are continuously hydrogenated to fatty alcohols in a fixed-bed reactor in the presence of hydrogen in excess and hydrogenation catalysts under static pressures of 50 to 300 bar and at temperatures of 160 to 320&deg; C. The liquid product is cooled and the excess hydrogen is returned to the reactor entrance by a gas circulation pump as a recycle gas after separation of the liquid product. The expense involved in cooling and reheating the recycle gas is eliminated without any reduction in the quality of the fatty alcohol produced providing the recycle gas is returned to the reactor entrance without reheating and the hydrogenation reaction is carried out under static pressures of at least 200 bar.

Process for the production of fatty alcohols

Discontinuous process for conducting a heterogeneously catalyzed reaction and installation for heterogeneously catalyzed manufacture of products

Process for the production of .alpha.-branched aliphatic monocarboxylic

A process for the production of triglycerides of C.sub.1 -C.sub.4 alkyl esters of C.sub.6 -C.sub.22 fatty acids:

Process for the production of triglycerides

A process for the production of solid or paste-form products by fast reactions is carried out stoichiometrically wherein a gaseous medium is introduced into each of the reactants to be reacted with one another, the reactant streams formed are combined and are subsequently forced through a spray unit in a weight ratio of gaseous medium to product stream of from 0.04 to 0.3 (kg/kg) and at a rate of 0.1 to 15 m/second, as calculated from the gas-free reactant streams and based on the free cross-section of the spray unit. The products obtained are free from readily volatile constituents.

Process for the production of solid or paste-form products

The invention relates to a process, more especially a discontinuous process, for conducting a reaction taking place at elevated temperature in which heat-sensitive products are formed. To increase the volume-time yield, a heat transfer unit independent of the reactor is used for heating. The invention also relates to an apparatus for the production of heat-sensitive products at elevated temperatures. This apparatus comprises a reactor and a heating system. To increase the volume-time yield, the heating system comprises at least one heat transfer unit arranged outside and connected to the reactor.

Process and apparatus for making a heat-sensitive material

The invention is a process for the continuous liquid-phase esterification of C.sub.2 -C.sub.24 fatty acids with alkanols in countercurrent contact and reaction in a reaction column, the catalysts and fatty acids are introduced at the top plate and the alkanols below the lowest plate, at a head pressure of the reaction column of 200 to 900 hPa. The process reduces dehydration of the alkanols.

Process for the continuous esterification of fatty acids

A process for the continuous transesterification of C.sub.6 -C.sub.22 fatty acid lower alkyl esters, particularly methyl esters, with polyhydric C.sub.2 -C.sub.5 alcohols, particularly glycerol, in a reaction column comprising a rectifying and reaction section, alkaline catalysts and polyhydric alcohol are introduced into the upper part of the reaction column and boiling fatty acid methyl ester is introduced into the middle part of the reaction column. The product collected in the sump of the column is removed, heated and returned to the lower part of the reaction column. Product is removed from the sump. Lower alkanols passing from the reaction column section to the rectifying section are rectified. The reaction column is operated in boiling equilibrium in its lower part and predominantly in an absorption/desorption equilibrium in its upper part.

Process for the continuous transesterification of fatty acid lower alkyl

A process for reducing the free fatty acid content of fats and oils by esterifying the free fatty acids with a lower monoalcohol in the presence of an acidic cation exchange resin as a solid esterification catalyst.

Process for the pre-esterification of free fatty acids in fats and oils

The epoxidation of terminally and/or internally olefinically unsaturated hydrocarbon compounds which are liquid at 50.degree. to 100.degree. C. and at atmospheric pressure (oil phase), in which the oil phase is treated with an acid phase containing acetic acid, hydrogen peroxide and peracetic acid in aqueous solution, after which the aqueous acid phase is separated from the oil phase, the peracetic acid in the aqueous acid phase is regenerated and the regenerated aqueous acid phase is returned to the epoxidation reactor. Epoxidation is carried out using an aqueous acid phase containing at most about 10% by weight of peracetic acid, and the peracetic acid content in the aqueous acid phase is reduced by at most about 50%, based on the peracetic acid content of the aqueous acid phase used, after a single passage through the epoxidation stage. After separation from the oil phase, the aqueous acid phase preferably is cooled before regeneration.

Process for the epoxidation of olefinically unsaturated hydrocarbon

In a multistage process for the continuous epoxidation of double bonds of terminal and non-terminal olefins containing more than 12 carbon atoms, unsaturated higher fatty acids and their lower alkanol and lower alkanediol esters and also unsaturated fatty alcohols containing from 8 to 18, preferably 18, carbon atoms and triglycerides of higher fatty acids including unsaturated fatty acids, preferably soyabean oil, using performic acid formed in situ from hydrogen peroxide and formic acid, the reactants, olefin and hydrogen peroxide/formic acid, are passed at ambient pressure in cross-counter flow through an at least three-stage reaction cascade. The olefinic phase is introduced into the first reaction stage, the hydrogen peroxide and the formic acid are introduced in separate streams into the penultimate reaction stage and the olefin phase and the hydrogen peroxide/formic acid phase (acid water phase) are separated from one another in a phase separator after each reaction stage. The olefinic phase passes successively through reaction stages I to n while the acid water, after reaction stage (n-1), passes through reaction stages (n-2) to 2 in counter flow to the olefin phase and then through stages n and 1, the reaction temperature being maintained in the range from 50.degree. to 80.degree. C. in the reactors and in the range from 15.degree. to 60.degree. C. in the phase separators.

Continuous process for the catalytic epoxidation of olefinic double

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Hilden, Germany

Eberhard Peukert