Oligomerization of C4 streams with very low 1 butene content

Patent metadata

Field	Value
Publication number	US-9682898-B2
Application number	US-201414901177-A
Country	US
Kind code	B2
Filing date	Jun 25, 2014
Priority date	Jun 27, 2013
Publication date	Jun 20, 2017
Grant date	Jun 20, 2017

Abstract

An OCTOL process is disclosed which by limitation of the conversion in its individual oligomerization steps is set up particularly for the productive utilization of C 4 feedstock mixtures with a low 1-butene content and which nevertheless yields a C 8 product mixture having an Iso index suitable for the preparation of plasticizer alcohols.

First claim

The invention claimed is:

1. A process for preparing a C 8 olefin or a C 12 olefin by oligomerization of butenes, comprising:
a) oligomerizing a portion of butenes present in a hydrocarbon mixture comprising a 2-butene and a further linear butene other than the 2-butene, to give one or more C 8 olefins and to give one or more C 12 olefins and optionally to give one or more C 12+ olefins, by contacting of the hydrocarbon mixture with an oligomerization catalyst arranged in a reaction zone, at a reaction temperature prevailing in the reaction zone, to give an oligomerizate comprising the prepared oligomers and one or more unreacted butenes;
b) removing the unreacted butenes from the oligomerizate; and
c) optionally, recycling a part of the removed unreacted butenes to the oligomerizing a);
wherein:
the sequence of a), b) and c) is carried out at least once with inclusion of the recycling c);
during the first time that the oligomerizing a) is carried out, a concentration of 1-butene in the hydrocarbon mixture, based on the concentration of linear butenes, is less than or equal to an equilibrium concentration of 1-butene, resulting from the reaction temperature of the sequence carried out for the first time, within the fraction of the linear butenes present in the hydrocarbon mixture during the first time;
the C 8 olefins are obtained as a C 8 product mixture whose Iso index is less than 1.2;
during the sequence carried out for the first time, the conversion of butenes, assessed directly over a first reaction zone, is limited to a first limit value of between 26.1 and 40 wt %; and
the limiting of the conversion in the oligomerization is accomplished by limiting the reaction temperature of the oligomerization to a maximum temperature of between 40° C. and 140° C.

2. The process of claim 1 , wherein:
the sequence of a), b) and c) is carried out at least two times one after another, and
in the second sequence carried out, the conversion of butenes, assessed directly at a second reaction zone, is limited to a second limiting value of between 5 and 50 wt %.

3. The process of claim 2 , wherein:
the sequence of a), b) and c) is carried out at least three times one after another, and
in the third sequence carried out, the conversion of butenes, assessed directly at a third reaction zone, is limited to a third limiting value of between 5 and 65 wt %.

4. The process of claim 3 , wherein:
the sequence of a), b) and c) is carried out at least four times one after another, and
in the fourth sequence carried out, the conversion of butenes, assessed directly at a fourth reaction zone, is limited to a fourth limiting value of between 5 and 80 wt %.

5. The process of claim 4 , wherein:
the sequence of a), b) and c) is carried out at least five times one after another, and
in the fifth sequence carried out, the conversion of butenes, assessed directly at a fifth reaction zone, is limited to a fifth limiting value of between 5 and 95 wt %.

6. The process of claim 1 , wherein an overall conversion of butenes achieved after all of the sequences of a), b) and c) have been carried out is between 5 and 100 wt %.

7. The process of claim 1 , wherein the limiting of the conversion in the oligomerization is accomplished by limiting the reaction temperature of the oligomerization to a maximum temperature of between 45° C. and 120° C.

8. The process of claim 1 , wherein more than 80 wt % of the oligomers prepared are C 8 olefins.

9. The process of claim 1 , wherein a composition of the C 8 olefins obtained is as follows, adding up to 100 wt %:
n-octenes: 10 to 25 wt %;
methylheptenes: 50 to 80 wt %;
dimethylhexenes: 10 to 30 wt %.

10. The process of claim 1 , wherein the C 8 product mixture has an Iso index of less than 1.1.

11. The process of claim 1 , wherein the hydrocarbon mixture in the sequence carried out for the first time is a reactant mixture having the following composition, which adds up to 100 wt %:
1-butene: less than 10 wt %;
2-butenes: 20 to 90 wt %;
isobutene: less than 5 wt %;
n-butane: less than 80 wt %;
isobutane: less than 80 wt %; and
others: less than 5 wt %.

12. The process of claim 1 , carried out in a plant within which exactly one reaction zone is assigned to each sequence carried out.

13. The process of claim 1 , wherein in each sequence apart from the last sequence, a non-recycled part of the removed unreacted butenes is provided as a hydrocarbon mixture for the subsequent step sequence.

14. The process of claim 13 , further comprising:
performing at least one selected from the group consisting of:
(a) totally hydrogenating the non-recycled part of the removed unreacted butenes in the last sequence, to obtain a butane mixture;
(b) oxidatively or non-oxidatively dehydrogenating the non-recycled part of the removed unreacted butenes in the last sequence, to obtain butadiene;
(c) hydroformylating the non-recycled part of the removed unreacted butenes in the last sequence, to obtain pentanals;
(d) oxidizing the non-recycled part of the removed unreacted butenes in the last sequence, to obtain maleic anhydride;
(e) metathesizing the non-recycled part of the removed unreacted butenes in the last sequence;

(f) hydrating the non-recycled part of the removed unreacted butenes in the last sequence, to obtain butanols;
(g) alkylating the non-recycled part of the removed unreacted butenes in the last sequence;
(h) isomerizing the non-recycled part of the removed unreacted butenes in the last sequence;
(i) carbonylating the non-recycled part of the removed unreacted butenes in the last sequence;
(j) cracking the non-recycled part of the removed unreacted butenes in the last sequence in a steamcracker or in a fluid-catalytic cracker, to obtain hydrocarbons having less than four carbon atoms; and
(k) combusting the non-recycled part of the removed unreacted butenes in the last sequence to give thermal energy.

15. The process of claim 1 , wherein oligomers obtained in individual sequences are combined and then separated into a C 8 product mixture, into a C 12 product mixture and into a C 12+ product mixture.

Assignees

• Peitz Stephan
• Geilen Frank
• Maschmeyer Dietrich
• Stochniol Guido
• Evonik Degussa Gmbh

Inventors

• Peitz Stephan
• Geilen Frank
• Maschmeyer Dietrich
• Stochniol Guido

Classifications

• C10G2300/1092

  C2-C4 olefins · CPC title

• C07C5/48

  with oxygen as an acceptor · CPC title

• C10G2400/22

  Higher olefins · CPC title

• C10G50/00

  Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation · CPC title

• C07C2521/04

  Alumina · CPC title