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Julius Montz Gmbh

Rasselstein Gmbh

Gerd Kaibel

Manfred Stroezel

Werner Aquila

Horst Hartmann

Udo Rheude

Franz-Josef Mueller

Carsten Oost

Ekkehard Schwab

Achim Stammer

Kaspar Bott

Walter Dobler

Ralf-Thomas Rahn

Jochem Henkelmann

Rolf Pinkos

Klaus Ebel

Klemens Flick

Hartwig Fuchs

Mathias Haake

Rolf Hartmuth Fischer

Herwig Hoffmann

Harald Rust

Hagen Jaedicke

Alois Kindler

Axel Nissen

Franz Josef Brocker

Klaus Breuer

Joaquim Henrique Teles

Wolfgang Harder

Martin Fischer

Klemens Massonne

Alexander Weck

Manfred Julius

Thomas Krug

Wolfgang Reif

Helmut Jansen

Frank Stein

Frank-Friedrich Pape

Arnd B&ouml;ttcher

Bram Willem Hoffer

Jan Kurt Eberhardt

Walter Rebafka

Martin Schäfer

Hartwig Voβ

Bernhard Bockstiegel

Wolfram Burst

Johann-Peter Melder

Wolfgang Siegel

Rainer Becker

Hartmut Hibst

Hans-Josef Sterzel

Rocco Paciello

Peter Bassler

Andreas Kramer

Boris Breitscheidel

Norbert Rieber

Peter Zehner

Walter Himmele

Rolf-Hartmuth Fischer

Karsten Eller

Georg Heinrich Grosch

Thomas Schaub

Holger Borchert

Frank Funke

Randolf Hugo

Andreas Ansmann

Michael Schulz

Michael Röper

Klaus Halbritter

Stefan Rittinger

Stephan Schlitter

Martin Merger

Till Gerlach

Franz J Broecker

Signe Unverricht

Holger Friedrich

Hans-Georg Goebbel

Florian Garlichs

Ulrich M&uuml;ller

Michael Steiniger

Matthias Dernbach

Joachim Pfeffinger

Rudolf Erich Lorenz

Bernd Heida

Tilman Sirch

Christoph Adami

Michael Slany

Frank Haese

Kurt Schneider

Daniel Schneider

Harald Laas

Josef Guth

Michael Horner

Jens Weiguny

Gunther Windecker

Eckhard Ströfer

Werner Hefner

Marcus Sigl

Reiner Sauer

Martin Sohn

Andreas Walch

Apparatus and processes for continuous distillative separation of a mixture comprising one or more alkanolamine(s) are described. The separation is performed in one or more dividing wall column(s) and the alkanolamine or the alkanolamines is/are withdrawn as a side draw stream or side draw streams (side fraction(s)).

Devices and method for continuous distillative separation of a mixture containing one or more alkanolamine(s)

In the acid-catalyzed esterification of mercaptoalkyl alcohols by means of carboxylic acids to form mercaptoalkly carboxylates, formation of undesirable, usually sparingly soluble by-products usually occurs. The process of the invention in the absence of acid catalysts avoids the formation of such by-products. Particularly when the esterification of the invention is carried out as reactive distillation using reactive column and residence vessel, good degrees of conversion can also be obtained without acid catalyst and at the same time the formation of the by-products can be largely avoided.

Process for preparing mercaptoalkyl carboxylates

Process for obtaining formic acid by thermal separation of a stream comprising formic acid and a tertiary amine (I), in which a liquid stream comprising formic acid and a tertiary amine (I) in a molar ratio of from 0.5 to 5 is produced by combining tertiary amine (I) and a formic acid source, from 10 to 100% by weight of the secondary components present therein are separated off and formic acid is removed by distillation in a distillation apparatus at a bottom temperature of from 100 to 300&#xb0; C. and a pressure of from 30 to 3000 hPa abs from the liquid stream obtained, the bottom discharge from the distillation apparatus being separated into two liquid phases and the upper liquid phase being recycled to the formic acid source and the lower liquid phase being recycled for separating off the secondary components and/or to the distillation apparatus.

Process for the preparation of formic acid

Apparatus and processes for continuous distillative separation of a mixture comprising one or more alkanolamine(s), wherein the separation is performed in one or more dividing wall column(s) and the alkanolamine or the alkanolamines is/are withdrawn as a side draw stream or side draw streams (side fraction(s)).

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

What is described is a process for obtaining maleic anhydride by distillation from a solution of maleic anhydride in a high-boiling absorbent which has been obtained by gas phase oxidation of a hydrocarbon and at least partial absorption of the oxidation products into the absorbent, by The maleic anhydride obtained as a side draw has a low content of acrylic acid and acetic acid.

Process for obtaining maleic anhydride by distillation

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 dividing wall column is described which includes the following segments: a) an upper column region (), b) an enrichment section () of the feed section, c) a stripping section () of the feed section, d) an upper part () of the offtake section, e) a lower part () of the offtake section, f) an intermediate region () of the feed section, g) an intermediate region () of the offtake section and h) a lower column region (). The dividing wall column has a dividing wall () is located vertically between the segments b) () and d) () and between the segments c) () and e) (). The segments b) (), d) (), c) () and e) () have separation-active internals, Segment b () has a cross-sectional area Awhich is at least 10% smaller than the cross-sectional area Aof segment d) (), and segment c) has a cross-sectional area Awhich is at least 10% greater than the cross-sectional area Aof segment e) ().

Dividing wall column for fractionation of a multicomponent mixture

The invention relates to a method for the separation of ascorbic acid from a mixture containing ascorbic acid and-keto-L-gulonic acid in a polar, preferably aqueous solvent, by means of liquid/liquid extraction using an amide. The method preferably also comprises steps for the back-extraction of the ascorbic acid, recycling of the extraction solvent and/or the back extraction solvent and for isolation of the ascorbic acid from the back extraction solvent. The invention further relates to a method for the production of ascorbic acid from KGA and isolation of the ascorbic acid so produced.

Method for the separation of ascorbic acid from a polar solvent containing ascorbic acid and 2-keto-L-gulonic acid

The invention relates to a process and apparatus for the isothermal operation of heterogeneously catalyzed reactions involving at least three phases in the form of a gaseous phase, a liquid phase and a solid phase. The invention provides apparatus for carrying out reactions involving a gaseous phase, a liquid phase and a solid phase, comprising (i) a dispersing element for dispersing a gas phase in a liquid phase to generate a reaction fluid, (ii) at least one reactor which possesses an inlet, an outlet and a reactor space bounded by heat-removing walls which are spaced apart substantially uniformly along the main flow axis of the reaction fluid, and which is fitted with catalyst-coated metal fabric, and (iii) a feed line which routes the reaction fluid from the dispersing element to the reactor inlet and is sufficiently short that the degree of dispersion of the reaction fluid does not substantially change in the course of the passage through the feed line.

Isothermal operation of heterogeneously catalyzed three phase reactions

A column is described for carrying out reactive distillations in the presence of a heterogeneous particulate catalyst having an ordered packing or random packings which form intermediate spaces in the column interior, the quotient of the hydraulic diameter for the gas flow through the ordered packing or the random packings and the equivalent diameter of the catalyst particles being in the range from 2 to 20, preferably in the range from 5 to 10, in such a manner that the catalyst particles are introduced into the intermediate spaces, distributed and discharged loose under the action of gravity.

Device and method for carrying out heterogeneously-catalysed reactive distillations in particular for the production of pseudoionone

A process is proposed for the distillation or reactive distillation of a mixture that includes at least one toxic component, the process being carried out in a column containing a structured packing, having at least one packing layer () having a lower end () and an upper end (), the packing layer having an internal geometry varying over its height, in such a manner that in the distillation or reactive distillation, in a first, lower region () of the packing layer () a bubbling layer having a predominantly disperse gas phase can be established and simultaneously in a second, upper region () of the packing layer () a film flow having a predominantly continuous gas phase can be established.

Method for carrying out the distillation or reactive distillation of a mixture containing at least one toxic constituent

The present invention relates to a process for the hydrogenation of substituted or unsubstituted, monocyclic or polycyclicaromatics to form the corresponding cycloaliphatics, in particular of benzene to cyclohexane, by bringing the aromatic into contact with a hydrogen-containing gas in the presence of a catalyst, where hydrogen in which residual gases are present is used.

Method for the hydrogenation of aromatic compounds with hydrogen containing residual gas

A process is described for preparing tetrahydrogeranylacetone in which pseudoionone, geranylacetone and/or dihydrogeranylacetone in a liquid phase, in which particles of a catalyst which is capable of preferentially hydrogenating carbon-carbon double bonds over carbon-oxygen double bonds are suspended, is conducted through a device which inhibits the transport of the catalyst particles in the presence of a hydrogen-containing gas.

Method for the production of tetrahydrogeranylacetone

A process for working up by distillation the crude products obtained in the process according to DE-A 196 07 954 and containing 1,6-hexanediol (HDO), 1,5-pentanediol (PDO) or caprolactone (CLO) in order to obtain the corresponding pure products, the working-up by distillation being carried out in each case in a dividing wall column (TK) in which a dividing wall (T) is arranged in the longitudinal direction of the column with formation of an upper common column region (), a lower common column region (), a feed section () having a rectification section () and stripping section (), and a take-off section () having a stripping section () and rectification section (), with feeding of the respective crude product HDO, PLO or CLO in the middle region of the feed section () and removal of the high boiler fraction (C) from the bottom of the column, of the low boiler fraction (A) via the top of the column and of the medium boiler fraction (B) from the middle region of the take-off section (), or in thermally coupled columns.

Method and device for the distillative processing of 1,6-hexanediol, 1,5-pentanediol and caprolactone

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Lampertheim, Germany

Gerd Kaibel