Basf Aktiengesellschaft

Basf Se Corporation

Basf Aktiengeselllschaft

Wilhelm Ruppel

Johann-Peter Melder

Klaus Joachim Mueller-Engel

Martin Dieterle

Ulrike Wegerle

Andreas Tenten

Claus Hechler

Goetz-Peter Schindler

Catharina Klanner

Wolfgang Gerlinger

Joaquim Henrique Teles

Otto Machhammer

Jochen Petzoldt

Thomas Fetzer

Heiko Arnold

Hans-Peter Neumann

Werner Hefner

Ulrich Hammon

Peter Bassler

Peter Zehner

Klaus Halbritter

Werner Aquila

Dirk Demuth

Anton Meier

Jens Weiguny

Hartwig Fuchs

Jochem Henkelmann

Wolfgang Siegel

Hermann Luyken

Wolfgang Harder

Norbert Rieber

Matthias Schwarzmann

Klaus Harth

Gerhard Olbert

Christian Walsdorff

Klaus Joachim Müller-Engel

Gerald Vorberg

Udo Rheude

Götz-Peter Schindler

Heinrich Aichinger

Grigorios Kolios

Peter Pfab

Petr Kubanek

Mark Duda

Karl-Heinz Ross

Wolfgang Mägerlein

Manfred Eggersdorfer

Sebastian Storck

Hans Martan

Michael Baier

Peter Resch

Hans-Juergen Bassler

Karl-Heinrich Klappert

Herbert Vogel

Helmuth Menig

Karl Siegfried Brenner

Heinz Rutter

Wolfgang Schneider

Thomas Genger

Andreas Walch

Christian Müller

Catharina Horstmann

Anne Wenzel

Anton Negele

Michael Becker

Karl-Heinz Boehning

Johannes E Schmidt

Michael Bender

Harro Wache

Michael Schönherr

Hermann Wistuba

Axel Deimling

Helmut Schmidtke

Eckhart Wagner

Albena Kostova

Bernhard Otto

Michael Schelper

Michael Kotter

Volker Vogt

Otto Woerz

Reinhard Körner

Beatrice Röβler-Feigel

Volker Schumacher

Walter Scheidmeir

Hans-Ulrich Scholz

Frederik Van Laar

Axel Salden

Rolf Seubert

Hans-Juergen Scheiper

Jasmina Kessel

Harald Schultheiss

Lothar Riekert

Uwe Behling

Wolfgang Gunkel

Guenther Achhammer

Godwind Tafara Peter Mabande

Günther Achhammer

Beatrice Rössler-Feigel

Otto Worz

Klaus-Joachim Mueller-Engel

The invention relates to a tube bundle reactor with a flat feed hood. Alternatively, the release hood may also have a flat design. The flat design reduces the heat of reaction which arises in the hood in the case of reaction types which take place not only in the tube bundle (uncatalyzed reactions and reactions with homogeneously distributed catalyst). This greatly suppresses undesired reactions which already take place in the hood owing to accumulated heat, which achieves a higher selectivity in the case of thermally sensitive reactions. In addition, the thermal distribution within the hoods can be controlled precisely. The tube bundle reactor comprises a tube bundle which has a feed end which is connected to a feed hood of the tube bundle reactor, wherein the feed hood is configured in a flat design with a cross-sectional area at the feed end and an internal volume, and the ratio of internal volume to cross-sectional area is less than 0.35 m. The invention is further implemented by means of a process for operating a tube bundle reactor, comprising: introducing a reactant mixture into a tube bundle and converting at least a proportion of the reactant mixture within the tube bundle to a product. The introducing comprises: feeding the reactant mixture into an interior of a feed hood of the tube bundle reactor and passing the reactant mixture on into a feed end of the tube bundle in the form of a fluid stream. The fluid stream has a cross-sectional area on entry into the feed end, and the interior of the feed hood through which the fluid stream flows has an internal volume; where the ratio of internal volume to cross-sectional area is less than 0.35 m.

Tube bundle reactor for uncatalyzed or homogeneously catalyzed reactions

The present patent application describes a method of regenerating a ruthenium catalyst for the hydrogenation of benzene, which comprises flushing the catalyst with inert gas in a regeneration step until the original activity or part of the original activity has been attained.

Method of regenerating ruthenium catalysts for the hydrogenation of benzene

A process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in a reactor which is manufactured from a composite material which consists, on its side in contact with the reaction chamber, of a steel B with specific elemental composition which, on its side facing away from the reaction chamber, either directly or via an intermediate layer of copper, or of nickel, or of copper and nickel, is plated onto a steel A with specific elemental composition, and also partial oxidations of the dehydrogenated hydrocarbon and the reactor itself.

Reactor for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated

A shell which encloses an interior and has at least one first orifice for feeding at least one gas stream into the interior and at least one second orifice for withdrawing a gas stream fed to the interior beforehand via the at least one first orifice from the interior, the surface of the shell, on its side in contact with the interior, being manufactured at least partly, in a layer thickness of at least 1 mm, from a steel which has a specific elemental composition, and in the interior, a process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated is carried out in a reactor which is manufactured from the steel on its side in contact with the reaction gas.

A reactor in the form of an essentially horizontal cylinder for carrying out an autothermal gas-phase dehydrogenation of a hydrocarbon-comprising gas stream by means of an oxygen-comprising gas stream to give a reaction gas mixture over a heterogeneous catalyst configured as monolith is disclosed herein. The interior of the reactor is divided by a detachable, cylindrical or prismatic housing which is arranged in the longitudinal direction of the reactor, gastight in the circumferential direction and open at two end faces of the housing into an inner region, having one or more catalytically active zones. In each case, a packing composed of monoliths may be stacked on top of one another, next to one another, and above one another and before each catalytically active zone. Also in each case, a mixing zone having solid internals and an outer region arranged coaxially to the inner region are provided.

Reactor for carrying out autothermal gas-phase dehydrogenations

A process for heterogeneously catalyzed partial dehydrogenation of a hydrocarbon, in which a reaction gas mixture input stream comprising the hydrocarbon to be dehydrogenated is conducted through a fixed catalyst bed disposed in a shaft and the reaction gas mixture input stream is obtained in the shaft by metering an input gas II comprising molecular oxygen upstream of the fixed catalyst bed into an input gas stream I which comprises molecular hydrogen and the hydrocarbon to be dehydrogenated and is flowing within the shaft toward the fixed catalyst bed.

Process for heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated

The present invention relates to a process for preparing at least one monocyclic ketone having from 4 to 20 carbon atoms by reacting a mixture Gcomprising at least one monocyclic olefin having from 4 to 20 carbon atoms with a mixture Gcomprising at least dinitrogen monoxide, wherein said reaction is performed adiabatically.

Process for preparing cyclic ketones

Process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated

A process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in a reactor which is manufactured from a steel with specific elemental composition on its side in contact with the reaction gas, and also partial oxidations of the dehydrogenated hydrocarbon and the reactor itself.

The present invention relates to a process for preparing hydrocyanic acid (HCN) by catalytic dehydration of gaseous formamide in a reactor which has an internal reactor surface made of a steel comprising iron and chromium and nickel, and also to a reactor for preparing hydrocyanic acid by catalytic dehydration of gaseous formamide, which reactor has an internal reactor surface made of a steel comprising iron and chromium and nickel, and also to the use of the reactor of the present invention in a process for preparing hydrocyanic acid by catalytic dehydration of gaseous formamide.

Hydrocyanic acid consisting of formamide

In a process for heterogeneously catalyzed partial gas phase oxidation of propene to acrolein, the starting reaction gas mixture is oxidized over a fixed catalyst bed which consists of at least two fixed catalyst bed zones and is accommodated in two successive temperature zones A, B, and the transition from temperature zone A to temperature zone B does not spatially coincide with a transition from one fixed catalyst bed zone to another fixed catalyst bed zone.

Heterogeneously catalyzed partial gas phase oxidation of propene to acrolein

Iron oxides are upgraded by calcining at from 700 to 1200&#xb0; C.

Iron oxides with a higher degree of refining

In a process for heterogeneously catalyzed partial gas phase oxidation of propene to acrylic acid, the propene-containing starting reaction gas mixture is oxidized in a first reaction stage using a fixed catalyst bed 1 which consists of a plurality of fixed catalyst bed zones and is accommodated in two successive temperature zones A, B, and the acrolein-containing product gas mixture of the first reaction stage is then oxidized in a second reaction stage using a fixed catalyst bed 2 which consists of a plurality of fixed catalyst bed zones and is accommodated in two successive temperature zones C, D, and the transition from one temperature zone to another temperature zone within one reaction stage does not spatially coincide with a transition from one fixed catalyst bed zone to another fixed catalyst bed zone.

Heterogeneously catalyzed partial gas phase oxidation of propene to acrylic acid

In a process for heterogeneously catalyzed partial gas phase oxidation of acrolein to acrylic acid, the starting reaction gas mixture is oxidized over a fixed catalyst bed 1 which consists of at least two fixed catalyst bed zones and is accommodated in two successive temperature zones A, B, and the transition from temperature zone A to temperature zone B does not coincide with a transition from one fixed catalyst bed zone to another fixed catalyst bed zone.

Heterogeneously catalyzed partial gas phase oxidation of acrolein to acrylic acid

Growing community of inventors

Mannheim, Germany

Wilhelm Ruppel