Bayer Aktiengesellschaft

Deutsche Gold- Und Silber-scheideanstalt Vormals Roessler

Helmut Waldmann

Wulf Schwerdtel

Hermann Seifert

Wolfgang Swodenk

Hans-Joachim Traenckner

Otto Immel

Gerd Schreyer

Gunter Prescher

Johann Grolig

Rolf Wirthwein

Otto Weiberg

Gebhard Rauleder

Zoltan Kricsfalussy

Gunter Stammann

Rudolf Braden

Gerhard Darsow

Manfred Hajek

Robert Becker

Hans-Ulrich Dummersdorf

Christoph Jupe

Uwe Westeppe

Willi Hofen

Fritz Gestermann

Carl Casser

Franz-Rudolf Minz

Klaus G Wilms

Natalja Zubritskaya

Anatoly Bazanov

Alexandre Timofeev

Gennady Terechtchenko

Ludwig Bottenbruch

Volker Serini

Klaus Nachtkamp

Herbert Klenk

Volker Mues

Gerd Fengler

Gerd-Michael Petruck

Jurgen Dahmer

Jurgen Baumert

Helmut Harle

Gunther Schummer

Hans-Josef Buysch

Dieter Freitag

Josef Pedain

Wolfgang Behrenz

Claus H Wulff

Lothar Puppe

Reinhard Langer

Hans-Helmut Schwarz

Christian Rasp

Wolfram Wagner

Kaspar Hallenberger

Klaus D Berg

Alfred Eitel

Gerhard Scharfe

Wolfgang Gau

Marko Zlokarnik

Harald Medem

Kurt Halcour

Reinhard Schomacker

Heinrich Steude

Bernd Griehsel

Gerd Siekmann

Wilfried Niemeier

Gerhard Friedhofen

J&uuml;rgen Schneider

Rupert Wenzel

Karl-Hermann Reissinger

Joachim Schneider

Christian Frohlich

Reinhard Schom Acker

Rolf Schalenbach

Helmut H&auml;rle

Hermann Seifer

Kurt-Wilheim Eichenhofer

In the process for working up the reaction gas consisting of chlorine, hydrogen chloride, oxygen and water vapour produced in a chlorine reactor, the reaction gas leaving the reactor is first cooled until the water of reaction and hydrogen chloride condense in the form of concentrated hydrochloric acid. The concentrated hydrochloric acid is then separated from the reaction gas in a phase separation column and discharged. The remaining reaction gas, from which the substantial proportion of the water and a proportion of the hydrogen chloride has been removed, is then post-dried in a drying tower The post-dried reaction gas consisting of chlorine, oxygen and hydrogen chloride is then compressed to 1 to 30 bar by a compressor In the subsequent stage, the compressed reaction gas is passed through a cooled chlorine recuperator wherein the chlorine is very largely liquefied. Finally, the components of the reaction gas which could not be condensed in the chlorine recuperator are at least partially returned to the reactor

Process for working up reaction gases during the oxidation HCI to chlorine

Diaminodipropyl ethers and hydroxyaminodipropyl ethers are prepared by catalytic amination of dipropylene glycol.

Process for the preparation of diaminodipropyl ethers and

In the method for the chemical reaction of gaseous educts, the educts are brought to reaction in a phase contact apparatus 1 in the presence of a catalytically active corrosive liquid. This corrosive liquid is delivered hydropneumatically in an intermittent cycle in the circuit from a sump vessel 4 connected to the lower end of the phase contact apparatus 1 to a supply vessel 9, connected to the upper end of the phase contact apparatus (delivery cycle), from which the corrosive liquid drains through the phase contact apparatus 1 and a connecting line 11 connected at its lower end and then collects in the sump vessel 4 (drainage cycle).

Method and device for delivering hot, aggressive media

The present invention relates to a process for preparing 2-methyl-2,4-diaminopentane by introducing acetone, ammonia and hydrogen into a two-zone reactor at a temperature of 20.degree. to 130.degree. C. and a pressure of 30 to 250 bar, wherein the first zone contains a cationic exchange resin containing NH.sub.4.sup..sym. groups or an aluminum oxide and/or silicon oxide catalyst and the second zone contains a hydrogenation catalyst containing nickel.

Process for the preparation of 2-methyl-2,4-diaminopentane

The present invention relates to a process for preparing 1,4-bis(aminomethyl)cyclohexane by reacting a 40 to 80 wt. % aqueous solution of 1,4-bis(hydroxymethyl)cyclohexane with a mixture of hydrogen and ammonia in the presence of a nickel/copper/chromium catalyst at a pressure of 100 to 250 bar and a temperature of 150.degree. to 250.degree. C.

Process for the preparation of 1,4-bis(aminomethyl) cyclohexane

In the method for the chemical reaction of gaseous educts the educts are brought to reaction in a phase contact apparatus 1 in the presence of a catalytically active corrosive liquid. This corrosive liquid is delivered hydropneumatically in an intermittent cycle in the circuit from a sump vessel 4 connected to the lower end of the phase contact apparatus 1 to a supply vessel 9, connected to the upper end of the phase contact apparatus (delivery cycle), from which the corrosive liquid drains through the phase contact apparatus 1 and a connecting line 11 connected at its lower end and then collects in the sump vessel 4 (drainage cycle).

C.sub.1 -C.sub.4 -Dialkyl carbonates can be obtained from the corresponding C.sub.1 -C.sub.4 -alkanols, carbon monoxide and oxygen by reacting these substances in the presence of Cu salts, the water of reaction being limited to less than 10 wt % in the reaction mixture by at least partial withdrawal.

Process for the preparation of dialky carbonates

The preparation of 4,4'-dinitrostilbene-2,2'-disulphonic acid by oxidation of 4-nitrotoluene-2-sulphonic acid with oxygen in alkaline medium in aqueous ether alcohol makes possible a simplified work-up.

Process for preparing 4,4'-dinitrostilbene-2,2'-disulphonic acid and its

Chlorinated aromatic compounds are dechlorinated in a simple and inexpensive manner by heating them to 300.degree. to 450.degree. C. in a salt melt in the presence of water and/or water vapor and carbon.

Process for the dechlorination of chlorinated aromatic compounds

The preparation of dimethyl carbonate by reaction of methanol, carbon monoxide and oxygen in the presence of Cu compounds is carried out in distillation units and the water of reaction is removed at least partially from the stripping region or the bottom phase.

Process for preparing dimethyl carbonate

Organic compounds are selectively oxidized by means of a particularly advantageous process, using elemental oxygen and a catalyst containing palladium and copper and carrying out the process in the presence of carbon monoxide.

Catalytic oxidation

Acylbenzenes of the formula ##STR1## can be prepared by reaction of benzene with carboxylic acids of the formula

Process for the preparation of acylbenzenes

A Pd catalyst in which an .alpha.- or .gamma.-Al.sub.2 O.sub.3 as support is first treated with at least one compound of the rare earth metals and with at least one compound of manganese and then with at least one palladium compound is suitable for the preparation of a mixture of optionally substituted cyclohexylamine and optionally substituted dicyclohexylamine by hydrogenation of a correspondingly substituted aniline.

Palladium catalyst and its use in the preparation of a mixture of

The plastic waste is reacted in a plasma reactor 3 under reducing conditions in a plasma containing substoichiometric oxygen at temperatures above 1200.degree. C. to form a plasma pyrolysis gas consisting of low molecular weight carbon fragments which is then cooled to temperatures below 1500.degree. C. The cooled plasma pyrolysis gas is then delivered in compressed form as a fuel of high calorific value and high temperature to a gas turbine 10 for generating power. The waste heat of this gas turbine is used to generate steam which is fed into a steam turbine 12 for generating more power. The process is suitable for plastic waste of any composition and leads to complete conversion into a gas of high calorific value so that a high exergetic efficiency level is achieved.

Process for converting plastic waste into power

Optionally substituted cyclohexylamine and optionally substituted dicyclohexylamine can be obtained by catalytic hydrogenation of optionally substituted aniline, a catalyst being employed which contains ruthenium, palladium or a mixture of both metals, which are applied to a support of niobic acid or tantalic acid or a mixture of both. The catalyst contains the noble metal(s) in a total amount from 0.05 to 5% by weight, relative to the total weight of the catalyst. In the case of the use of both noble metals, their weight ratio to one another is 1:9-9:1.

Process for the preparation of a mixture of cyclohexylamine and

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Leverkusen, Germany

Helmut Waldmann