Basf Se Corporation

Basf Aktiengesellschaft

Basf Corporation

Basf Se (ellwanger & Baier Patentanwälte)

Karlsruhe Institute of Technology

Peter Pfab

Hermann Luyken

Tobias Aechtner

Jens Scheidel

Robert Baumann

Gerd Haderlein

Wolfgang Siegel

Michael Bartsch

Tim Jungkamp

Peter Bassler

Gerhard Olbert

Grigorios Kolios

Andreas Johann Schmidt

Matthias Georg Schwab

Johann-Peter Melder

Alfred Oftring

Andreas Deckers

Goetz-Peter Schindler

Qi Fu

Barbara K Slawski

Alexander Weck

Randolf Hugo

Wilhelm Ruppel

Markus Weber

Ulrike Wegerle

Heiner Schelling

Klaus Schubert

Otto Watzenberger

Sebastian Ahrens

Joachim Pfeffinger

Ralf Boehling

Andreas Leitner

Petra Deckert

Albena Kostova

Volker Krase

Weiqing Joe Zou

David James Brockway

Regina Benfer

Andrea Haunert

Eckhard Ströfer

Boris Buschhaus

Wolfgang Gerlinger

Thomas Genger

Gerhard Laqua

Matthias Kloetzer

Gordon Brasche

Andreas Otterbach

Thomas Schneider

Dieter Franz

Peter Baβler

Peter Wahl

Dieter Stützer

Jasmina Kessel

Andreas Glass

Alireza Rezai

Godwind Tafara Peter Mabande

Dirk Groβschmidt

Frank Kleine Jäger

Dieter Starosta

Verena Weiskopf

Guenther Achhammer

Manfred Kraut

Stefan Hannemann

Jochen Götz

Aristides Morillo

Matthias Kl&ouml;tzer

Tobias ÄChtner

Godwin Tafara Peter Mabande

Disclosed herein is a chromium oxide catalyst composition having reduced levels of chromium (VI), methods of making a chromium oxide catalyst composition and system, and illustrative uses of the chromium oxide catalyst composition and system. The catalyst disclosed may be a gel and may comprise chromium(III) oxide and chromium(VI) oxide at an amount of about 10,000 ppm or less based on total chromium oxide contents in the chromium oxide catalyst composition.

Chromium catalyst, its preparation and use

The present disclosure relates to processes for formation of a molecular sieve, particularly a metal-promoted molecular sieve, and more particularly an Iron(III) exchanged zeolite. Preferably, the zeolite is of the chabazite form or similar structure. The processes can include combining a zeolite with Iron(III) cations in an aqueous medium. The process can be carried out at a pH of less than about 7, and a buffering material can be used with the aqueous medium. The processes beneficially result in Iron exchange that can approach 100% along with removal of cations (such as sodium, NH, and H) from the zeolite. An Iron(III)-exchanged zeolite prepared according to the disclosed processes can include about 2,000 ppm or less of cation and about 1% by weight or greater of Iron(III). The disclosure also provides catalysts (e.g., SCR catalysts) and exhaust treatment systems including the Iron(III)-exchanged zeolite.

Process for preparing iron(III)-exchanged zeolite composition

Disclosed herein is a chromium oxide catalyst composition having reduced levels of chromium (VI), methods of making a chromium oxide catalyst composition and system, and illustrative uses of the chromium oxide catalyst composition and system. The catalyst disclosed may be a gel and may comprise chromium (III) oxide and chromium (VI) oxide at an amount of about 10,000 ppm or less based on total chromium oxide contents in the chromium oxide catalyst composition.

The present disclosure relates to processes for formation of a molecular sieve, particularly a metal-promoted molecular sieve, and more particularly an Iron(III) exchanged zeolite. Preferably, the zeolite is of the chabazite form or similar structure. The processes can include combining a zeolite with Iron(III) cations in an aqueous medium. The process can be carried out at a pH of less than about 7, and a buffering material can be used with the aqueous medium. The processes beneficially result in Iron exchange that can approach 100% along with removal of cations (such as sodium, NH4, and H) from the zeolite. An Iron(III)-exchanged zeolite prepared according to the disclosed processes can include about 2,000 ppm or less of cation and about 1% by weight or greater of Iron(III). The disclosure also provides catalysts (e.g., SCR catalysts) and exhaust treatment systems including the Iron(III)-exchanged zeolite.

The present invention relates to a process for purifying adiponitrile (ADN), wherein crude ADN is introduced into a rectification apparatus (R). The rectification apparatus (R) comprises a first side draw and preferably also a second side draw, the first side draw being disposed below the crude ADN introduction point and the optional second side draw being disposed above the crude ADN introduction point. The first side draw is used to draw off a gaseous stream comprising ADN while the optional second side draw is used to draw off undesired by-products such as 1-amino-2-cyanocyclopentene (ACCP) which are often generated in ADN production and consequently may be present in the crude ADN. The gaseous stream from the first side draw of (R) is introduced into a second rectification apparatus (R). (R) is used to separate off ADN from remaining high boilers and any other by-products present, pure ADN being drawn off from (D) as overhead product. It is preferable when the process according to the invention employs crude ADN from a reaction of butadiene with hydrocyanic acid (HCN).

Method for purifying adipodinitrile (ADN)

A process is described for preparing 3-pentenenitrile, characterized by the following process steps:

Method for producing linear pentenenitrile

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

The invention relates to a method of production of catalyst particles, comprising platinum and tin and also at least one further element, selected from lanthanum and cesium, on zirconium dioxide as support, comprising the steps: preparation of one or more solutions containing precursor compounds of Pt, Sn and at least one further element of La or Cs and also ZrO, converting the solution(s) to an aerosol, bringing the aerosol into a directly or indirectly heated pyrolysis zone, carrying out pyrolysis, and separation of the particles formed from the pyrolysis gas. Suitable precursor compounds comprise zirconium(IV) acetylacetonate, lanthanum(II) acetylacetonate and cesium acetate, hexamethyldisiloxane, tin 2-ethylhexanoate, platinum acetylacetonate, zirconium(IV) propylate in n-propanol and lanthanum(II) acetylacetonate. The invention also relates to the catalyst particles obtainable using the method according to the invention, and to the use thereof as dehydrogenation catalysts.

Catalyst from flame-spray pyrolysis and catalyst for autothermal propane dehydrogenation

The invention relates to a process for preparing triethylenetetramine substituted by at least one methyl group (Me-TETA or methyl-substituted TETA compounds). Me-TETA is prepared by hydrogenating biscyanomethylimidazolidine (BCMI) in the presence of a catalyst. The present invention further relates to methyl-substituted TETA compounds as such. The present invention further relates to the use of methyl-substituted TETA compounds as a reactant or intermediate in the production of, for example, coatings or adhesives.

Methyl-substituted teta compounds

A process for isomerizing cis-2-pentenenitrile to 3-pentenenitriles, by isomerizing cis-2-pentenenitrile with amidines, tertiary amines or mixtures thereof as a catalyst at temperatures of 80 to 200&#xb0; C. and a pressure of 0.01 to 50 bar.

Process for isomerizing CIS-2-pentenenitrile to 3-pentenenitriles

The invention relates to a process for workup of a stream () comprising butene and/or butadiene, butane, hydrogen and/or nitrogen and carbon dioxide, comprising:

Process for workup of a stream comprising butene and/or butadiene

A method for producing 3-pentenenitrile is provided that includes: (a) isomerizing an educt stream containing 2-methyl-3-butenenitrile on at least one dissolved or dispersed isomerization catalyst to form a stream (1), which contains the isomerization catalyst(s), 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z)-2-methyl-2-butenenitrile; (b) distilling the stream (1) to obtain a stream (2) as the overhead product, which contains 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z)-2-methyl-2-butenenitrile and a stream (3) as the bottom product, which contains the isomerization catalyst(s); (c) distilling the stream (2) to obtain a stream (4) as the overhead product, which is enriched with (Z)-2-methyl-2-butenenitrile in comparison to stream (2), and a stream (5) as the bottom product, which is enriched with 3-pentenenitrile and 2-methyl-3-butenenitrile in comparison to stream (2); (d) distilling stream (5) to obtain a stream (6) as the bottom product, which contains 3-pentenenitrile and a stream (7) as the head product containing 2-methyl-3-butenenitrile.

An process for preparing 3-pentenenitrile by hydrocyanating 1,3-butadiene, in which the process yield with regard to recycled 1,3-butadiene is maximized.

Method for producing 3-pentenenitrile by means of the hydrocyanation of 1,3-butadiene

A process for extractively removing homogeneously dissolved catalysts from a reaction effluent of a hydrocyanation of unsaturated mononitriles to dinitriles with a hydrocarbon H, including performing the steps of a) concentrating the reaction effluent before step b) by distillation at pressures of from 0.1 to 5000 mbar and temperatures of from 10 to 150&#xb0; C., b) adding a hydrocarbon H to the concentrated reaction effluent to obtain a stream I, and c) feeding stream I, without prior separation of the liquid phases, into an extraction apparatus and extracting it at a temperature T with the hydrocarbon H to obtain a stream II comprising the hydrocarbon H enriched with the catalyst and a stream III having a low catalyst content.

Extraction of nickel (0) complexes from nitrile mixtures with reduced rag formation

Method of producing compounds of the general formulaXPR(OR)&#x2003;&#x2003;Iawhere X is chlorine, bromine or iodine and Ris an organic radical, by reacting compounds of the general formulaXPR&#x2003;&#x2003;II,in which X has the meaning given above and Ris an organic radical, with compounds of the general formulaROH&#x2003;&#x2003;III,in which Rhas the meaning given above, to give a mixture IV, in that

Method for producing organic phosphorous compounds containing halogens

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Neustadt, Germany

Peter Pfab