Basf Aktiengesellschaft

Basf Se Corporation

Frank Stein

Rolf Hartmuth Fischer

Rolf Pinkos

Rolf-Hartmuth Fischer

Michael Hesse

Boris Breitscheidel

Alexander Weck

Holger Borchert

Harald Rust

Stephan Schlitter

Ralf-Thomas Rahn

Rainer Becker

Karsten Eller

Christoph Sigwart

Thomas Krug

Shelue Liang

Klaus-Dieter Plitzko

Gerd Kaibel

Stephan Andreas Schunk

Ulrich M&uuml;ller

Markus Rösch

Karl Gerhard Baur

Joachim Wulff-Döring

Sylvia Huber

Martin Gall

Thomas Nöbel

Markus R&ouml;sch

Johann-Peter Melder

Ulrich Mueller

Manfred Julius

Oliver Bey

Norbert Asprion

Wolfgang Mägerlein

Gabriele Iffland

Michael Jolyon Sprague

Matthias Kummer

Joachim Wulff-D&ouml;ring

Kevin Huyghe

Stefanie Werland

Maarten Moors

Thomas N&ouml;bel

A process for preparing ethylamines and monoisopropylamine (MIPA), in which bioethanol is reacted with ammonia in the presence of hydrogen and of a heterogeneous catalyst to give ethylamines, said bioethanol having a content of sulfur and/or sulfur compounds of &#x2267;0.1 ppm by weight (calculated S), and then isopropanol is reacted with ammonia in the presence of the same catalyst and in the presence of hydrogen to give MIPA.

Process for preparing ethylamines and monoisopropylamine (MIPA)

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

A catalyst for the hydrogenation of C-dicarboxylic acids and/or their derivatives, preferably maleic anhydride, in the gas phase comprises from 5 to 100% by weight, preferably from 40 to 90% by weight, of copper oxide and from 0 to 95% by weight, preferably from 10 to 60% by weight, of one or more metals or compounds thereof selected from the group consisting of Al, Si, Zn, Pd, La, Ce, the elements of groups III A to VIII A and groups I A and II A as active composition applied in the form of a thin layer to an inert support material.

Catalytic coating for the hydrogenation of maleic anhydride and related compounds to give &#x3b3;-butyrolactone, tetrahydrofuran and derivatives thereof

In a process for preparing alcohols by catalytic hydrogenation of carbonyl compounds over a catalyst comprising rhenium on activated carbon, the catalyst used comprises rhenium (calculated as metal) in a weight ratio to the activated carbon of from 0.0001 to 0.5, platinum (calculated as metal) in a weight ratio to the activated carbon of from 0.0001 to 0.5 and, if appropriate, at least one further metal selected from among Zn, Cu, Ag, Au, Ni, Fe, Ru, Mn, Cr, Mo, W and V in a weight ratio to the activated carbon of from 0 to 0.25, and the activated carbon has been nonoxidatively pretreated. It is also possible to prepare ethers and lactones if the hydrogen pressure is not more than 25 bar. In this case, the activated carbon in the catalyst may also have been nonoxidatively pretreated.

Catalytic hydrogenation over rhenium-containing catalysts supported on activated carbon

C-dicarboxylic acids or derivatives thereof are hydrogenated in the gas phase in a fluidized-bed reactor. It is possible to use catalyst compositions known per se.

Method for the hydrogenation of maleic anhydride and related compounds in a fluid bed reactor

In a process for preparing alcohols by catalytic hydrogenation of carbonyl compounds over a catalyst comprising rhenium on activated carbon, the catalyst used comprises rhenium (calculated as metal) in a weight ratio to the activated carbon of from 0.0001 to 0.5, platinum (calculated as metal) in a weight ratio to the activated carbon of from 0.0001 to 0.5 and, if appropriate, at least one further metal selected from among Zn, Cu, Ag, Au, Ni, Fe, Ru, Mn, Cr, Mo, W and V in a weight ratio to the activated carbon of from 0 to 0.25, and the activated carbon has been nonoxidatively pretreated It is also possible to prepare ethers and lactones if the hydrogen pressure is not more than 25 bar. In this case, the activated carbon in the catalyst may also have been nonoxidatively pretreated.

Method for catalytic hydrogenation on rhenium-containing active carbon carrier catalysts

The present invention relates to a process for the gas-phase hydrogenation of C -dicarboxylic acids and/or their derivatives over a catalyst based on copper oxide to give substituted or unsubstituted &ggr;-butyrolactone and/or tetrahydrofuran, which comprises, which a first reaction zone in which the C -dicarboxylic acid and/or its derivatives is/are reacted to give a mixture comprising a substituted or unsubstituted &ggr;-butyrolactone as main product and a subsequent second reaction zone in which the substituted or unsubstituted &ggr;-butyrolactone present in the mixture from the first hydrogenation step is reacted at a temperature lower than the temperature in the first hydrogenation step to give substituted or unsubstituted tetrahydrofuran.

Method for the hydrogenation of maleic anhydride and related compounds in two serial reaction zones

Unsubstituted or alkyl-substituted THF is obtained by catalytic hydrogenation in the gas phase of C -dicarboxylic acids and/or their derivatives using a catalyst comprising <80% by weight, preferably <70% by weight, in particular from 10 to 65% by weight, of CuO and >20% by weight, preferably >30% by weight, in particular from 35 to 90% by weight, of an oxidic support having acid centers, at a hot spot temperature of from 240 to 310&deg; C., preferably from 240 to 280&deg; C., and a WHSV over the catalyst of from 0.01 to 1.0, preferably from 0.02 to 1, in particular from 0.05 to 0.5, kg of starting material/l of catalyst x hour.

Method for the production of tetrahydrofuran

Method for producing hexanediol

Method for producing cyclopentanone

A process for the preparation of 1,6-hexanediol and 6-hydroxycaproic acid or esters thereof by catalytic hydrogenation of adipic acid, adipic acid monoesters or adipic acid diesters or streams of starting material which contain adipic acid or esters thereof as essential constituents, in which the bottom product obtained in the distillation of the hydrogenation product, following removal of the hexanediol and hydroxycaproic acid or esters thereof, and essentially comprises oligomeric esters of 6-hydroxycaproic acid, is recycled to the hydrogenation, and the resulting mixture of starting material and recycle stream is reacted at from 100 to 300&deg;C., at from 10 to 300 bar in the liquid phase and at a molar ratio of carboxyl groups to be hydrogenated to hydrogen in the reactor of from 1:5 to 1:100 on hydrogenation catalysts is described.

Method for producing 1,6-hexanediol and 6-hydroxycaproic acid or their esters

Method for producing 1,6-hexanediol

A process for polymerizing cyclic ethers over a heterogeneous catalyst comprises using a heterogeneous catalyst comprising one or more pillared interlayered clays (PILCs).

Method for polymerizing cyclic ether

A process for preparing cyclopentanone and cyclopentene-1-carboxylic acid or an ester thereof of the formula I

Method for producing cyclopentanone and cyclopentene-1-carboxylic acid and their esters

Hexanediol is prepared by hydrogenating dialkyl adipates or mixtures which contain a dialkyl adipate as the essential component and organic halogen compounds as impurities, by a process in which, before the hydrogenation, the dialkyl adipates or the mixtures containing dialkyl adipates are passed at from 50 to 250&deg; C. and from 1 to 100 bar over copper catalysts which have a copper content, calculated as CuO, of from 0.5 to 80% by weight, a surface area of from 5 to 1500 m,/g, a porosity of from 0.05 to 1.5 cm,/g and a copper surface area of from 0.1 to 20 m,/g, in order to remove the organic halogen compounds.

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Bad Dürkheim, Germany

Frank Stein