Abstract: The invention concerns fire-extinguishing and/or fire-retarding compositions comprising at least one water-absorbing polymer and at least one alkali metal salt of a nonpolymeric saturated carboxylic acid, processes for their production and the use of the compositions for firefighting or as fire-retarding coatings.

Abstract: The invention concerns fire-extinguishing and/or fire-retarding compositions comprising at least one water-absorbing polymer and at least one alkali metal salt of a nonpolymeric saturated carboxylic acid, processes for their production and the use of the compositions for firefighting or as fire-retarding coatings.

Abstract: The invention relates to a liquid distributor in the form of a channel distributor with drainage outlets. To ensure that the uniformity of distribution of the liquid is largely independent of disturbance factors, for example blockages of the drainage outlets, the drainage outlets are in the form of drainage pipes having a cross-section which tapers in the shape of a nozzle. The inner wall of the nozzle-like tapering of the drainage outlets being made of plastic, or another material resistant to the adherence of solids which would block the flow of liquid through the outlet.

Abstract: A liquid distributor, for a substantially vertical reactor with a fixed bed catalyst, in the form of a channel distributor with drainage outlets and further comprising an internal cleaning mechanism with cleaning elements to be lowered into the openings of the drainage outlets, is disclosed.

Abstract: A method for the removal of a spent catalyst from a fixed-bed reactor is disclosed, wherein a suction hose, in which a high pressure hose comprising a high-pressure nozzle is integrated, is introduced into the reactor, the catalyst is then size-reduced by water under high pressure passed through the nozzle, the catalyst/water mixture is removed under suction and is optionally collected in a separator.

Abstract: The invention is an improved palladium-containing catalyst and process for preparing the catalyst. The catalyst is prepared by impregnating a dry activated carbon with a pH above 8 with a solution of palladium salt, separating the aqueous phase from the impregnated activated carbon when the aqueous phase has reached a pH of at least 1 and reducing the palladium which is supported on the activated carbon.

Abstract: The invention relates to a process for the hydrogenation of native fats, oils and fat derivatives, such as fatty acids and fatty acid esters, to fatty alcohols in a fixed-bed reactor, more particularly in co-current, hydrogen being recirculated in a stoichiometric excess, more particularly in an excess of 10 to 100 fold, and the fat, oil or fat derivative passing through the reactor only once. To minimize the specific hydrogen demand without having to accept significant losses in regard to specific reactor load, product selectivity and catalyst life, the hydrogen is passed successively through at least two fixed-bed reactors 4,10 without the gas issuing from the reactors 4 and entering the following reactors 10 being cooled and the fat, oil or fat derivative is simultaneously introduced into the reactors 4,10.

Abstract: The invention relates to the use of colloidal, stabilized silica sol as an auxiliary for stabilizing and/or increasing the activity of catalysts which show a tendency towards activity-reducing sintering under high-temperature conditions.

Abstract: The invention relates to a process for the catalytic hydrogenation of liquid saturated and unsaturated C.sub.6-24 fatty acid methyl esters for the production of saturated fatty alcohols and methanol in the presence of gaseous hydrogen and hydrogenation catalysts under pressures of 50 to 300 bar and at temperatures in the range from 160.degree. to 250.degree. C., characterized in that the hydrogenation reaction is carried out in a tube bundle reactor in which isothermal conditions are established by a cooling or heating fluid, the liquid phase and gas phase being passed together as a co-current trickle phase over catalyst packings in the individual tubes of the reactor without any back-mixing, and in that the load per unit volume of the reaction is between 0.2 and 2.5 liters starting material per liter reactor volume per hour and the load per unit area of each individual tube of the reactor is between 1.5 and 24 m.sup.3 starting material per m.sub.

Abstract: 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.

Abstract: 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.

Abstract: Process for the production of a new copper (II) chromite spinel catalyst using colloidal silica gel and to its use for the direct fixed-bed hydrogenation of fatty acids to fatty alcohols of corresponding chain length.

Abstract: Process for the production of a new copper (II) chromite spinel catalyst using colloidal silica gel and to its use for the direct fixed-bed hydrogenation of fatty acids to fatty alcohols of corresponding chain length.

Abstract: An insecticidally active fraction is obtained from black pepper by a process comprising the following steps:(a) extraction of black pepper in ground form with CO.sub.2 at 30 to 70.degree. C. and 150 to 500 bar;(b) removal of sharp tasting fractions therein in a first expansion step at 25 to 35.degree. C. and 70 to 150 bar;(c) removal of an oily fraction containing the insecticidally active components as well as most of the essential oils in a second expansion step at 15 to 30.degree. C. and 40 to 70 bar;(d) removal of essential oils by steam distillation, and if desired;(e) hydrogenation of the insecticidally active components.

Abstract: A process for the stabilization of particulate, activated catalyst masses after the activation of the starting catalyst masses in a gas stream, wherein the particulate, activated catalyst masses are removed from the activation reactor in an inert gas atmosphere into a liquid alcohol or a mixture of two or more alcohols which are straight-chain or branched-chain alcohols containing from 6 to 12 carbon atoms in the alkyl radical, stabilizing the catalyst masses by impregnation with the alcohol or the alcohol mixture, optionally storing and/or transporting the alcohol-impregnated catalyst masses, removing excess alcohol, sieving the alcohol-moist catalyst mass, and introducing the catalyst mass into a catalysis reactor to form a catalyst filling.