Basf Se Corporation

Hans-Guenter Wagner

Sven Crone

Lothar Karrer

Heinz Ruetter

Kam Wing Wong

Christoph Bayer

Patrik Pietz

Markus Eggersmann

Gerrit Waters

Thomas Roussiere

Suman Thotla

Markus Neudert

Michael Huebner

Randolf Hugo

Randolph Hugo

Wolfgang Rohde

Stefan Bitterlich

Beatrice Röβler-Feigel

Qiang Miao

Gauthier Luc Maurice Averlant

Guenther Kirchner

Gabriele Zimmer

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reaction mixture () from the etherification unit () in the first distillation unit (), a C4-hydrocarbon raffinate being withdrawn as the overhead product (), and the alkyl tert-butyl ether being withdrawn as the bottom product (); (c) vaporizing the bottom product from the first distillation unit () in an evaporator () obtaining a vapor stream (); (d) reacting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distilling the reaction mixture () from the ether cleavage unit () in the second distillation unit (), isobutene being withdrawn as the overhead product (), the primary alcohol and diisobutene being withdrawn as the bottom product () and being recycled to the etherification unit (); wherein a purge stream () containing high boiling components with a normal boiling point higher than that of the alkyl tert-butyl ether is withdrawn from the evaporator () in step (c).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 (), this feed stream () being split up in at least three byproduct streams wherein a first byproduct stream () is rich in diisobutene, a second byproduct stream () is rich in the primary alcohol, and a third byproduct stream () is rich in components with a normal boiling point higher than 110° C.

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 ().

The invention relates to a process for starting up a plant for removing isobutene from an isobutene-containing C4-hydrocarbon mixture, the plant comprising an etherification unit containing moist acidic ion exchange resin, a first distillation unit, an ether cleavage unit, and a second distillation unit. The invention further relates to a process for shutting down the plant from a stationary operation mode.

Process for starting up and shutting down a plant for removing isobutene from a C4-hydrocarbon mixture

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

In a process for the cooligomerization of olefins, an olefin starting material comprising olefins having n carbon atoms and olefins having 2n carbon atoms is reacted over an olefin oligomerization catalyst to give a reaction product. The process is carried out under such conditions that the conversion of olefins having 2n carbon atoms is less than 10%. Both the cooligomer having 3n carbon atoms and the olefin having 2n carbon atoms which has been separated off from the reaction product have a high hydroformylatability.

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Neuleiningen, Germany

Hans-Guenter Wagner