Basf Se Corporation

Basf Aktiengesellschaft

Randolf Hugo

Johann-Peter Melder

Kirsten Dahmen

Alfred Oftring

Katrin Baumann

Thilo Hahn

Kirsten Wenz

Sabine Jourdan

Robert Baumann

Hermann Luyken

Gerd Kaibel

Thomas Preiss

Sebastian Ahrens

Jörg Pastre

Boris Buschhaus

Gordon Brasche

Alexander Weck

Stephanie Jaegli

Rupert Wagner

Jens Baldamus

Hardo Siegel

Dieter Hermeling

Bernd Heida

Gerrit Waters

Hans-Guenter Wagner

Thomas Roussiere

Suman Thotla

Sabine Huber

Michael Huebner

Thomas S Holst

Peter Bassler

Peter Pfab

Peter Lechtken

Peter Hammes

Uwe Stabel

Werner Peschel

Markus Neudert

Christoph Grossmann

Michael Jödecke

Rolf Wambsganβ

Hans-Peter Schmid

Harry Zachmann

Michael Jäger

Michael JÖDECKE

The invention relates to a process for obtaining isobutene from an isobutene containing C4-hydrocarbon mixture () in a plant comprising an etherification unit (), a first distillation unit (), an ether cleavage unit () and a second distillation unit (), the process comprising: (a) contacting the C4-hydrocarbon mixture () with a primary alcohol () and reacting the mixture with the primary alcohol in the presence of an acidic catalyst to form the corresponding alkyl tert-butyl ether in the etherification unit (); (b) distilling the reaction mixture () from the etherification unit () in the first distillation unit (), a C4-hydrocarbon raffinate being withdrawn as the overhead product (), and the alkyl tert-butyl ether being withdrawn as the bottom product (); (c) vaporizing the bottom product from the first distillation unit () in an evaporator () obtaining a vapor stream (); (d) reacting the vapor stream () of step (c) in the presence of an acidic catalyst obtaining isobutene and the primary alcohol as reaction products in the ether cleavage unit (); (e) distilling the reaction mixture () from the ether cleavage unit () in the second distillation unit (), isobutene being withdrawn as the overhead product (), the primary alcohol and diisobutene being withdrawn as the bottom product () and being recycled to the etherification unit (); wherein a purge stream () containing high boiling components with a normal boiling point higher than that of the alkyl tert-butyl ether is withdrawn from the evaporator () in step (c).

Process for obtaining isobutene from a C4-hydrocarbon mixture

The invention relates to a process for obtaining isobutene from an isobutene containing C4-hydrocarbon mixture () in a plant comprising an etherification unit (), a first distillation unit (), an ether cleavage unit () and a second distillation unit (), the process comprising: (a) contacting the C4-hydrocarbon mixture () with a primary alcohol () and reacting the mixture with the primary alcohol in the presence of an acidic catalyst to form the corresponding alkyl tert-butyl ether as an intermediate product and diisobutene as a by-product in the etherification unit (): (b) distilling the reaction mixture () from the etherification unit () in the first distillation unit (), a C4-hydrocarbon raffinate being withdrawn as the overhead product (), the alkyl tert-butyl ether and diisobutene being withdrawn as the liquid or vaporous bottom product (), and vaporizing the bottom product () if it is withdrawn as a liquid: (c) reacting the vaporous bottom product () in the presence of an acidic catalyst obtaining isobutene and the primary alcohol as reaction products in the ether cleavage unit (): (d) distilling the reaction mixture () from the ether cleavage unit () in the second distillation unit (), isobutene being withdrawn as the overhead product (), the primary alcohol and diisobutene being withdrawn as the bottom product () and being recycled to the etherification unit (); the plant further comprising a byproduct separation unit () being fed by a bottom purge stream () of the first distillation unit () and/or by a part of the bottom product of the second distillation unit (), wherein a diisobutene product stream rich in diisobutene is separated from this feed stream ().

A process for preparing EDDN and/or EDMN by conversion of FA, HCN and EDA, the reaction being effected in the presence of water, and, after the conversion, water being depleted from the reaction mixture in a distillation column, which comprises performing the distillation in the presence of an organic solvent which has a boiling point between water and EDDN and/or EDMN at the distillation pressure existing in the column or which forms a low-boiling azeotrope with water.

Process for preparing EDDN and EDMN

A process for reacting formaldehyde cyanohydrin (FACH) with ethylenediamine (EDA) in a reactor with limited backmixing at a temperature in the range from 20 to 120&#xb0; C., wherein the residence time in the reactor is 300 seconds or less.

Process for preparing EDDN and/or EDMN by conversion of FACH and EDA

A process is disclosed for separating the output from the reaction of EDDN or EDMN with hydrogen in the presence of THF, a catalyst, TETA or DETA, water, and optionally organic compounds having higher and lower boiling points than TETA or DETA. Hydrogen is removed, and the output is supplied to a distillation column DK1 in which an azeotrope, optionally comprising organic compounds with a boiling point lower than TETA or DETA, is removed from the top. A product comprising TETA or DETA is removed from the bottom and passed into a distillation column DK2, removing THF. A stream comprising TETA or DETA passes from the bottom of DK2. The DK1 azeotrope is condensed. Phase separation is induced by the addition of an organic solvent essentially immiscible with water, and the mixture is separated. The organic phase is recycled into DK1 and the water phase is discharged.

Process for working up reaction outputs from the hydrogenation of EDDN or EDMN

A process for reacting ethylenediamine-formaldehyde adduct (EDFA) and/or ethylene-diamine-monoformaldehyde adduct (EDMFA) with hydrogen cyanide (HCN) in a reactor with limited backmixing at a temperature in the range from 20 to 120&#xb0; C., wherein the residence time in the reactor is 300 seconds or less.

Process for preparing EDDN and/or EDMN by reacting EDFA and/or EDMFA with HCN

The present invention relates to a mixture of ethylenediamine (EDA) and N-methylethylenediamine (Me-EDA) with a low content of Me-EDA, which comprises at least 99.5% by weight of ethylenediamine, and wherein the concentration of N-methylethylenediamine is in the range from 0.005 to 0.15% by weight. The present invention further relates to a process for distillative workup of a mixture comprising EDA, Me-EDA and water, by introducing the mixture into a distillation column which is operated at a column top pressure of 10 mbar to 4 bar, wherein the weight ratio of water to ethylenediamine in the mixture used is a*X:Y where X is the proportion by weight of water and Y is the proportion by weight of ethylenediamine at the azeotropic point of a binary mixture of water and ethylenediamine at the column top pressure in question, and a is a real number with a value of 0.9 or more. The present invention further provides a process for preparing a distillable mixture comprising EDA, Me-EDA and water, which is suitable for preparing EDA with a low Me-EDA content.

Method for distilling mixtures comprising ethylenediamine, N-methylethylenediamine, and water, and mixtures of ethylenediamine and N-methylethylenediamine having a low content of N-methylethylenediamine obtainable thereby

Mixtures of hydrocarbons predominantly having 4 carbon atoms per molecule known as Ccuts are used in obtaining crude 1,3-butadiene by a thermal cracking process. Vaporous purified crude Ccuts are produced from liquid crude Ccuts, containing butanes, butenes, 1,3-butadiene, Chydrocarbons, Coligomers and polymers, and Chydrocarbons via an extractive distillation by fist removing the Coligomers and polymers and the Chydrocarbons and then vaporizing the liquid crude Ccut in a vaporizer vessel. The vaporizer vessel is directly or indirectly in contact with a stripping column where liquid Ccuts are supplied to the upper region, direct gas and liquid exchange with the vaporizer vessel occurs in the lower region, and vaporous purified crude Ccuts are removed from the top region.

Process for providing a vaporous purified crude C4 cut as a feed steam for an extractive distillation with a selective solvent

Secondary streams in 1,3-butadiene processing plants still contain high amounts of valuable 1,3-butadiene. An energy-efficient process for purifying a recycle stream from a 1,3-butadiene processing plant is provided. The recycle stream is divided into two substreams: the first substream for prepurifying pure 1,3-butadiene feedstream by removing high boilers relative to 1,3-butadiene in a stripping column and the second substream in an extractive distillation plant.

Process for purifying a recycle stream from a 1,3-butadiene processing plant

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

The invention relates to a process for preparing tetraethylenepentamine (TEPA) by hydrogenation of diethylenetriaminediacetonitrile (DETDN) over a catalyst. If appropriate, DETDN can also be present as a constituent of an amino nitrile mixture which additionally comprises diethylenetriaminemonoacetonitrile (DETMN).

Method for producing tetraethylenepentamine

The invention relates to a process for preparing triethylenetetramine (TETA), which, comprises the following steps:

Method for producing TETA by means of EDDN

The invention relates to a process for preparing an amino nitrile mixture comprising aminoacetonitrile (AAN) and from 5 to 70% by weight of iminodiacetonitrile (IDAN), which comprises heating crude AAN which is largely free of formaldehyde cyanohydrin (FACH-free) at a temperature of from 50 to 150&#xb0; C.

Method for producing aminonitriles

A process comprising: continuously distilling a crude xylylenediamine in a column to form a pure xylylenediamine and a bottom product, wherein the column comprises a distillation column having a side draw and the distillation column is operated under a reduced pressure and a bottom temperature of 185&#xb0; C. or less; drawing off the pure xylylenediamine from the side draw; evaporatively concentrating the bottom product of the distillation column in an additional evaporation stage to form a condensate; and returning the condensate into the distillation column.

Processes for preparing pure xylylenediamine

In a method for removing acid gases from a fluid stream, the fluid stream, which is in contact with an absorption medium within an absorber, is passed through a first absorption zone in the absorber to remove a majority of acid gases from the fluid stream. The fluid stream is susequently passed through a second absorption zone in the absorber to further remove acid gases from the fluid stream. The loaded absorption medium is passed into a first regeneration zone to obtain a partially regenerated absorption medium, and a part of the partially regenerated absorption medium is passed into the first absorption zone. The other part of the partially regenerated absorption medium is passed into a second regeneration zone to obtain a regenerated absorption medium. A part of the regenerated absorption medium is passed into the first absorption zone and the other part is passed into the second absorption zone.

Method for removing acid gases from a fluid stream

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Dirmstein, Germany

Randolf Hugo