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Udo Rheude

Joachim Paust

Manfred Stroezel

Gerd Kaibel

Hansgeorg Ernst

Walter Dobler

Manfred Julius

Erhard Henkes

Jochem Henkelmann

Ekkehard Schwab

Eckhard Hickmann

Wolfgang Krause

Werner Aquila

Ralf-Thomas Rahn

Bram Willem Hoffer

Jan Kurt Eberhardt

Mathias Haake

Johann-Peter Melder

Joaquim Henrique Teles

Wolfgang Siegel

Hartmut Hibst

Norbert Rieber

Thomas Krug

Wilhelm Ruppel

Harald Rust

Hagen Jaedicke

Alois Kindler

Christof Wilhelm Wigbers

Maximilian Vicari

Petr Kubanek

Dirk Demuth

Karl-Heinz Ross

Wolfgang Mägerlein

Bernhard Schulz

Heinz Etzrodt

Martin Rudloff

Dietmar Weller

Helmut Schmidtke

Ralph Versch

Uwe Leyk

Oliver Buβmann

Juergen Frank

Hartwig Voβ

Michael Karcher

Rudolf Erich Lorenz

Roman Dostalek

Franz Josef Brocker

Joachim Meyer

Melanie Brunner

Michael John

Matthias Kiefer

Carsten Oost

Wolfram Burst

Klaus Breuer

Joachim U Schneider

Christian Tragut

Luise Spiske

Wolfgang Bewert

Christian Knoll

Horst Schumacher

Peter Munster

Melanie Pahl

Nina Challand

Melanie Maas-Brunner

Oliver Bussmann

Arno Kochner

G&uuml;nter Wegner

Otto Worz

Juan Aiscar

Wolfgang Gunkel

Ulrich Schafer-Luderssen

J&ouml;rg Niekerken

Gunter Dauwel

Armin Bertram

Guenter Gaus

Helmut Berrsche

Ulrich Horcher

Ulrich H&ouml;rcher

Gerhard Ruf

A process continuously hydrogenating unsaturated compounds, in which particles of a first hydrogenation catalyst are suspended in a liquid phase in which an unsaturated compound is dissolved, the liquid phase, in the presence of a hydrogenous gas at a first partial hydrogen pressure and at a first temperature, is conducted through a packed bubble column reactor in cocurrent counter to the direction of gravity, the effluent from the bubble column reactor is sent to a gas-liquid separation, the liquid phase is sent to a crossfiltration to obtain a retentate and a filtrate, the retentate is recycled into the bubble column reactor and the filtrate, in the presence of a hydrogenous gas at a second partial hydrogen pressure and at a second temperature, is passed over a bed of a second hydrogenation catalyst, the second partial hydrogen pressure is at least 10 bar higher than the first partial hydrogen pressure.

Process for continuous hydrogenation or hydrogenating amination

Process for preparing 1,4-bishydroxyethylpiperazine (BHEPIP) of the formula I wherein diethanolamine (DEOA) of the formula II is reacted in the liquid phase in a reactor at a temperature in the range from 130 to 300&#xb0; C. in the presence of a copper-comprising, chromium-free heterogeneous catalyst.

Process for preparing 1,4-bishydroxyethylpiperazine

Processes for the continuous fractional distillation of a mixture containing morpholine (MO), monoaminodiglycol (ADG), ammonia and water from a reaction of diethylene glycol (DEG) with ammonia, the process including: (i) separating off ammonia from the mixture at a top of a first distillation column K; (ii) feeding a bottom fraction from Kto a second distillation column K, in which water and an organic product are separated off at the top at a temperature at the top in the range from 45 to 198&#xb0; C. and a pressure in the range from 0.1 to 15 bar; (iii) feeding a bottom fraction from Kto a third distillation column K, wherein the column Kis a dividing wall column (DWC)which preferably has a dividing wall (DW) in the longitudinal direction of the column to form an upper combined column region (), a lower combined column region (), an inflow part () having an enrichment section () and a stripping section (), and also an offtake part () having an enrichment section () and a stripping section (), with the bottoms from Kbeing fed in in the upper or middle third of the inflow part (), based on the number of theoretical plates of the inflow part, ADG and organic products having a boiling point of &#x3e;190&#xb0; C. (1.013 bar) being discharge at the bottom, organic products having a boiling point of &#x2266;128&#xb0; C. (1.013 bar) being discharge at a top and MO being discharge from the middle or lower third of the offtake part () (side offtake), based on the number of theoretical plates of the offtake part.

Method for the continuous separation by distillation of mixtures that contain morphonline (MO), monoaminodiglycol (ADG), ammonia and water by means of distillation

Processes for the continuous fractional distillation of a mixture comprising morpholine (MO), monoaminodiglycol (ADG), ammonia and water from a reaction of diethylene glycol (DEG) with ammonia, the process comprising: (i) separating off ammonia from the mixture at a top of a first distillation column K; (ii) feeding a bottom fraction from the first distillation column to a second distillation column K, wherein water and an organic product are separated off at a top of the second distillation column at a top temperature of 45 to 198&#xb0; C. and a pressure in the range from 0.1 to 15 bar; (iii) feeding a bottom fraction from the second distillation column to a third distillation column K, wherein morpholine and an organic product having a boiling point of &#x3c;140&#xb0; C. (1.013 bar) are separated off at a point selected from a top and a side offtake of the third distillation column, and monoaminodiglycol and an organic product having a boiling point of &#x3e;190&#xb0; C. (1.013 bar) are separated off at a bottom of the third distillation column, and (iv) feeding the morpholine-comprising stream from the third distillation column to a fourth column K, wherein morpholine is separated off at a side offtake of the fourth column, an organic product having a boiling point of &#x2266;128&#xb0; C. (1.013 bar) is separated off at a top of the fourth distillation column and an organic product having a boiling point of &#x2267;128&#xb0; C. (1.013 bar) is separated off at a bottom of the fourth distillation column.

Method for the continuous separation of mixtures comprising morpholine (MO), monoaminodiglycol (ADG), ammonia and water by means of distillation

Process for the continuous fractional distillation of mixtures including morpholine (MO), monoaminodiglycol (ADG), ammonia and water obtained by reaction of diethylene glycol (DEG) with ammonia, which includes separating off ammonia at the top of a first distillation column K10, feeding the bottoms from K10 to a second distillation column K20 in which water and organic products are separated off at the top at a temperature at the top in the range from 45 to 198&#xb0; C. and a pressure in the range from 0.1 to 15 bar, feeding the bottoms from K20 to a third distillation column K30 in which MO and organic products having a boiling point of &#x3c;140&#xb0; C. (1.013 bar) are separated off at the top or at a side offtake and ADG and organic products having a boiling point of &#x3e;190&#xb0; C. (1.013 bar) are separated off at the bottom, feeding the MO including stream which is separated off at the top or at a side offtake of the column K30 to a fourth column K40 in which organic products having a boiling point of &#x2266;128&#xb0; C. (1.013 bar) are separated off at the top and MO and organic products having a boiling point of &#x2267;128&#xb0; C. (1.013 bar) are separated off at the bottom and the bottoms from K40 are fed to a fifth distillation column K55 in which MO is separated off at the top and organic products having a boiling point of &#x2267;128&#xb0; C. (1.013 bar) are separated off at the bottom.

Processes for continuous fractional distillation of mixtures comprising morpholine, monoaminodiglycol, ammonia and water

A process is described for continuously hydrogenating unsaturated compounds, in which particles of a first hydrogenation catalyst are suspended in a liquid phase in which an unsaturated compound is dissolved, the liquid phase, in the presence of a hydrogenous gas at a first partial hydrogen pressure and at a first temperature, is conducted through a packed bubble column reactor in cocurrent counter to the direction of gravity, the effluent from the bubble column reactor is sent to a gas-liquid separation, the liquid phase is sent to a crossfiltration to obtain a retentate and a filtrate, the retentate is recycled into the bubble column reactor and the filtrate, in the presence of a hydrogenous gas at a second partial hydrogen pressure and at a second temperature, is passed over a bed of a second hydrogenation catalyst, wherein the second partial hydrogen pressure is at least 10 bar higher than the first partial hydrogen pressure.

A process for preparing at least one unsaturated alcohol (B) comprises the steps (I) to (III) below:

Method for preparing acetylene alcohols and their secondary products

A process is proposed for preparing C acetate for Vitamin A synthesis by hydroformylation of 3,4-diacetoxybut-1-ene (3,4-DABE), according to which a 3,4-DABE is used which is obtained by acetoxylation of 1,3-butadiene with acetic acid and air in the presence of a catalyst and removing by distillation the 3,4-DABE formed in this case as by-product.

Process for preparing C5 acetate

Method for producing butyrolactones

Process for preparing higher unsaturated ketones

Process for the continuous preparation of &agr;- and/or &bgr;-ionone or homologous compounds using concentrated sulfuric acid at temperatures from 20 to 90&deg; C., in the presence of organic solvents or diluents with cooling and by subsequent termination of the reaction by hydrolysis of the reaction mixture with water or dilute sulfuric acid, wherein both the cyclization of pseudoionones and the subsequent hydrolysis of the reaction mixture are carried out in a virtually adiabatic reaction in one or more reaction mixing pump(s) which are connected in series and each of which consists essentially of a rotationally symmetrical mixing chamber formed from a peripheral wall and two end walls and of a mixing rotor made of material inert to sulfuric acid and with rotational drive, where the mixing chamber has at least one inlet opening for each component and one outlet opening for the reaction mixture, and annular channels in fluid connection to one another in the end walls, and wherein the heat of the two reactions is in each case partly or wholly removed with the aid of a downstream heat exchanger.

Process for preparing ionones

Method for producing enol ethers

A process for preparing 4-hydroxy-1,2,2-trimethylcyclopentyl methyl ketones of the general formula I, in particular of the (1R,4S)-4-hydroxy-1,2,2-trimethylcyclopentyl methyl ketone of the formula Ia ##STR1## which is required for preparing the red dye capsorubin which is in demand, starts from 2,2,6-trimethylcyclohexanones of the general formula II ##STR2## where R is hydrogen or a protective group, via the novel intermediates of the general formulae V and VI ##STR3## by diastereoselective epoxidation and reaction of the resulting 7-oxabicyclo[4.1.0]heptanes of the general formula VIII ##STR4## with Lewis acids and, where appropriate, removal of the protective group. Also claimed are the novel intermediates of the formula V and their (1S) and (1R) isomers and those of the formula VIII as well as their (1R,3S,6S), (1S,3S,6R) and (1R,3R,6S) isomers.

Preparation of (1R,4S)-4-hydroxy-1,2,2-trimethylcyclopentyl methyl

In a process for carrying out an exothermal reaction, selected from the addition reaction of organomagnesium halide compounds to carbonyl compounds and the ensuing hydrolysis of the addition product, a considerable fraction of the heat liberated during the reaction is removed by evaporation of the solvent.

Reacting Grignard compounds with carbonyl compounds and ensuing

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Otterstadt, Germany

Udo Rheude