Basf Se Corporation

Basf Aktiengesellschaft

Basfaktiengesellschaft

Sven Crone

Götz-Peter Schindler

Mark Duda

Lothar Karrer

Hans-Guenter Wagner

Heinz Ruetter

Christoph Bayer

Patrik Pietz

Kam Wing Wong

Markus Eggersmann

Frieder Borgmeier

Catharina Klanner

Gerhard Olbert

Andreas Brodhagen

Thorsten Johann

Franz Corr

Ekkehard Schwab

Wolfgang Mackenroth

Petr Kubanek

Rainer Papp

Regina Benfer

Marcus Sigl

Frederik Van Laar

Joachim-Thierry Anders

Karl Hoelemann

Klaus Joachim Mueller-Engel

Rocco Paciello

Otto Machhammer

Alexander Weck

Wolfgang Rohde

Hartwig Voss

Goetz-Peter Schindler

Stefan Bitterlich

Thomas Hill

Christoph Adami

Ansgar Gereon Altenhoff

Armin Diefenbacher

Ralf Boehling

Georg Degen

Thomas Mackewitz

Roland Krokoszinski

Frank Poplow

Heinrich-Josef Blankertz

Martin Volland

Markus Schmitt

Frank Heimann

Till Blum

Dag Wiebelhaus

Falk Simon

Frank Kiesslich

Thomas Holtmann

Jochen Buerkle

Karl Hölemann

Christoph Obler

Oliver Ryll

Guenther Kirchner

Gabriele Zimmer

Thomas Heldemann

Disclosed is a process for the regeneration of an adsorber. For the regeneration a liquid stream (S) is applied which is obtained by hydrogenation of a stream (S) comprising at least one alkane and least one olefin. The stream (S) comprises one alkane and a reduced amount of at least one olefin compared to the amount in the stream (S). Then the stream (S) is converted from the liquid into the gaseous phase and the adsorber is regenerated by contact with the gaseous stream (S).

Process for adsorber regeneration

Disclosed is a process for the regeneration of an adsorber (A). The adsorber (A) is regenerated by contact with a gaseous stream (S) and the outflow of the adsorber (A) comprising condensate of stream (S) and organic composition (OC) collected in a device. After regeneration of the adsorber (A) the stream (S) in the adsorber (A) is replaced completely or at least partially by the content of the device. Then the adsorber (A) is fed with organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulfur.

Product recovery process for adsorber regeneration

Disclosed is a process for the purification of an organic composition (OC) by adsorption using an assembly containing at least two adsorbers. The organic composition (OC) comprising at least one alkane, at least one olefin and at least one compound containing oxygen and/or sulphur is fed into a first adsorber (A) of the assembly in order to obtain an organic composition (OC) comprising at least one alkane, at least one olefin and a reduced amount of at least one compound containing oxygen and/or sulphur compared to the respective amount in organic composition (OC). Hydrogenation of the organic composition (OC) provides a stream (S) comprising at least one alkane and a reduced amount of at least one olefin compared to the respective amount in organic composition (OC) obtained after feeding into the first adsorber (A). A second adsorber (A) of the assembly is regenerated by contact with stream (S).

Process for purification of an organic composition

A process for the production of oligomerized olefins comprising the following steps: purification of an organic composition (OC) in at least one adsorber to obtain an organic composition (OC); oligomerization of organic composition (OC) in the presence of a catalyst to obtain an organic composition (OC); distillation of organic composition (OC) in a distillation column (D1) to obtain an organic composition (OC) from the upper part of (D) and an organic composition (OC) from the lower part of (D); hydrogenation of organic composition (OC) to obtain an organic composition (OC) and regeneration of an adsorber (A) employing organic composition (OC) as regeneration media.

Process for the production of oligomerized olefins

The invention relates to a process for the regeneration of an adsorber. For the regeneration a liquid stream (S) comprising at least one alkane is converted from liquid phase into gaseous phase. Then the adsorber is regenerated and heated by contact with gaseous stream (S) up to 230 to 270&#xb0; C. Subsequently, the adsorber is cooled first by contact with gaseous stream (S) to a temperature of 90 to 150&#xb0; C. followed by cooling with liquid stream (S) to a temperature below 80&#xb0; C. The outflow of the adsorber (S*) during the cooling with gaseous stream (S) and optionally the outflow of the adsorber (S*) during cooling with liquid stream (S) is recycled in at least one of these steps.

Recycling process for adsorber regeneration

The invention relates to a process for regeneration of an adsorber (A) by contact with a stream (S), wherein the stream (S) is heated in advance by at least two heat exchange units (HEU) and (HEU). As outflow of the adsorber (A) a stream (S) is obtained, which is passed through at least two heat exchange units (HEU) and (HEU) traversed by stream (S), wherein the temperature of stream (S) fed into each heat exchange unit is higher than the temperature of stream (S) fed into the heat exchange units (HEU) and (HEU), in order to directly transfer heat from stream (S) to stream (S).

Heat exchange process for adsorber regeneration

The present invention relates to a process for preparing hydroformylation products of olefins having at least four carbon atoms, in which a high proportion of both the linear C-olefins having a terminal double bond comprised in the olefin-comprising feed used and of the linear C-olefins having an internal double bond is converted into hydroformylation products. Furthermore, the invention relates to a process for preparing 2-propylheptanol which comprises such a hydroformylation process.

Method for the hydroformylation of olefins

A method is proposed for providing an oxygen-containing gas stream for the endothermic reaction of an initial stream comprising one or more hydrocarbons, having a predetermined oxygen concentration and a predetermined temperature, wherein a fluid fuel stream

Method for providing an oxygen-containing gas stream for the endothermic reaction of an initial stream comprising one or more hydrocarbons

A process for preparing oligomers by continuous oligomerization of butenes is described, wherein a) a feed stream 1) comprising 1-butene and 2-butene in a total concentration of from 10 to 70% by weight and from 10 to 60% by weight of isobutane is reacted until more than 60% by weight of the 1-butene comprised in the feed stream 1 but less than 50% by weight of the 2-butene comprised in feed stream 1 have been converted into oligomers. b) The oligomers obtained in a) are separated off and optionally passed to a further work-up and the remaining residual stream is fed to work-up by distillation. c) Isobutane is separated off by distillation from the residual stream, and d) the isobutane-depleted stream obtained after the work-up by distillation c) is reacted to form oligomers.

Process for preparing oligomers of butene

A process for heterogeneously catalyzed partial direct oxidation of propane and/or isobutane, in which target product is removed in a workup stage from the product gas mixture obtained in the reaction stage, the remaining residual product gas mixture is divided into two portions of the same composition, one portion is recycled into the reaction stage and the other portion is discharged, and both the reaction stage and the workup stage are operated at elevated pressure.

Heterogeneously catalyzed partial direct oxidation of propane and/or isobutane

A process for preparing butadiene, comprising A) providing a stream (a) comprising n-butane; B) feeding stream (a) comprising into at least one first dehydrogenation zone and nonoxidatively catalytically dehydrogenating n-butane to obtain a stream (b) comprising n-butane, 1-butene, 2-butene, butadiene, hydrogen and low-boiling secondary constituents; C) feeding stream (b) and an oxygenous gas into at least one second dehydrogenation zone and oxidatively dehydrogenating n-butane, 1-butene and 2-butene to obtain a stream (c) comprising n-butane, 2-butene, butadiene, low-boiling secondary constituents, carbon oxides and steam, wherein stream (c) has a higher content of butadiene than stream (b); D) removing the low-boiling secondary constituents and steam to obtain a stream (d) substantially consisting of n-butane, 2-butene and butadiene; E) separating stream (d) into a stream (e1) consisting substantially of n-butane and 2-butene and a stream (e2) consisting substantially of butadiene by extractive distillation; F) recycling stream (e1) into the first dehydrogenation zone.

Method for producing butadiene from n-butane

A reactor for carrying out a reaction between two fluid starting materials over a catalyst bed with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 ms in a mixing-in device, wherein the mixing-in device is made up of the following elements which are arranged essentially transverse to the inflow direction of the first fluid starting material stream:

Reactor for carrying out a reaction between two fluid starting materials over a catalyst bed with premixing of the fluid starting materials in a mixing-in device

A process for aminating hydrocarbons with ammonia, wherein the Ncontent in the mixture at the reactor exit is less than 0.1% by volume based on the total volume of the mixture at the reactor exit.

Direct amination of hydrocarbons

A reactor for carrying out a continuous oxydehydrogenation of a feed gas stream of saturated hydrocarbons after premixing with an oxygen-comprising gas stream over a moving catalyst bed which is introduced in the longitudinal direction of their reactor between two concentric cylindrical holding devices so as to leave a central interior space and an intermediate space between the moving catalyst bed and the interior wall of the reactor to give a reaction gas mixture, wherein the reactor has two or more reactor sections which are separated from one another by disk-shaped deflection plates arranged alternately in the central interior space and divided in subregions by annular deflection plates arranged in the intermediate space between the moving catalyst bed and the interior wall of the reactor, in each case with a mixing-in device which is located upstream of the moving catalyst bed in the flow direction of the reaction gas mixture and comprises the following elements:

Reactor for carrying out a continuous oxydehydrogenation and process

A process for preparing alkanols (I) selected from the group consisting of isopropanol and 2-butanol from the corresponding alkanes (II) selected from the group consisting of propane and n-butane, comprising the steps of:

Process for preparing isopropanol and 2-butanol from the corresponding alkanes

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Sven Crone