USRE45240EActiveUtilityPatentIndex 47

Process for preparing pure triethanolamine (TEOA)

Assignee: BASF SEPriority: Dec 19, 2008Filed: Dec 10, 2009Granted: Nov 11, 2014

Est. expiryDec 19, 2028(~2.5 yrs left)· nominal 20-yr term from priority

Inventors:MELDER JOHANN-PETER CAUWENBERGE GUNTHER VAN FREMAU TOM MOORS JÜRGEN HAHN THILO STEIN BERND

C07C 213/10

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Claims

Abstract

A process for preparing pure triethanolamine (TEOA) by continuously distillatively separating an ethanolamine mixture comprising TEOA and diethanolamine (DEOA), by distilling off DEOA in a distillation column (DEOA column) and supplying the resulting bottom stream comprising TEOA to a downstream column (TEOA column) in which the pure TEOA is withdrawn as a side draw stream, wherein the residence time of the ethanolamine mixture in the bottom of the DEOA column is <20 minutes.

Claims

exact text as granted — not AI-modified

The invention claimed is:

1. A process for preparing pure triethanolamine (TEOA) by continuously distillatively separating an ethanolamine mixture comprising TEOA and diethanolamine (DEOA), comprising distilling off DEOA in a distillation column (DEOA column) and supplying the resulting bottom stream comprising TEOA to a downstream column (TEOA column) in which the pure TEOA is withdrawn as a side draw stream, wherein the residence time of the ethanolamine mixture in the bottom of the DEOA column is &lt;20 minutes.

2. The process according to claim 1 , wherein the residence time of the ethanolamine mixture in the bottom of the DEOA column is &lt;15 minutes.

3. The process according to claim 1 , wherein the residence time of the ethanolamine mixture in the bottom of the DEOA column is in the range from 3 to &lt;12 minutes.

4. The process according to claim 1 , wherein the DEOA is withdrawn in the DEOA column as a side draw stream.

5. The process according to claim 1 , wherein the DEOA is withdrawn in a purity of ≧99.3% by weight.

6. The process according to claim 1 , wherein the TEOA of the TEOA column is withdrawn in a purity of ≧99.3% by weight.

7. The process according to claim 1 , wherein a product stream comprising ≧60% by weight of DEOA and ≦40% by weight of TEOA is withdrawn at the top of the TEOA column.

8. The process according to claim 1 , wherein the product stream withdrawn at the top of the TEOA column is recycled into the DEOA column.

9. The process according to an claim 1 , wherein the TEOA obtained in the side draw in the TEOA column is distilled in a further downstream column and removed there via the top.

10. The process according to claim 1 , wherein the TEOA column is a dividing wall column.

11. The process according to claim 1 , wherein the ethanolamine mixture comprising TEOA and DEOA for separation has been obtained beforehand by reacting ammonia with ethylene oxide in the liquid phase and subsequently removing NH 3 , water and monoethanolamine (MEOA).

12. The process according to claim 1 , wherein phosphorous acid or hypophosphorous acid or a derivative of one of these acids is added to the ethanolamine mixture for separation.

13. The process according to claim 1 wherein the pure TEOA has an APHA color number of ≦20.

14. The process according to claim 1, wherein the DEOA column is operated at a temperature in the bottom in the range from 170° C. to 200° C.

15. The process according to claim 1, wherein the ethanolamine mixture comprising TEOA and DEOA is fed into the side of the DEOA column.

16. The process according to claim 1, wherein the TEOA column is operated at a temperature in the bottom on the range from 170° C. to 200° C.

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