Method for producing ethyleneamines

Patent metadata

Field	Value
Publication number	US-11214535-B2
Application number	US-201816619987-A
Country	US
Kind code	B2
Filing date	May 24, 2018
Priority date	Jun 9, 2017
Publication date	Jan 4, 2022
Grant date	Jan 4, 2022

Abstract

The invention relates to processes for preparing alkanolamines and ethyleneamines in the liquid phase, by reacting ethylene glycol and/or monoethanolamine with ammonia in the presence of an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, wherein the amination catalyst is obtained by reductive calcination of a catalyst precursor. The catalyst precursor here is preferably prepared by contacting a conventional or catalytic support material with one or more soluble compounds of the active metals and optionally one or more soluble compounds of added catalyst elements. The present invention further relates to a process for preparing an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, the amination catalyst being obtained by reductive calcination of a catalyst precursor, wherein the reactor in which the catalyst precursor is reductively calcined is connected to a denox plant, and to the use of a denox plant in the preparation of amination catalysts.

First claim

The invention claimed is:

1. A process for preparing alkanolamines and/or ethyleneamines in a liquid phase, by reacting ethylene glycol and/or monoethanolamine with ammonia in the presence of an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, wherein the preparation of the amination catalyst consisting essentially of the following steps:
(i) preparing a catalyst precursor by contacting a conventional or catalytic support material with one or more soluble compounds of the active metals and optionally one or more soluble compounds of added catalyst elements;
(i)(a) optionally a work-up step comprising one or more of the steps of separation, washing and drying;
(ii) reductively calcining the catalyst precursor obtaining in step (i), where the reductive calcination is effected in the presence of hydrogen and the oxygen content in the reductive calcination is less than 0.1% by volume;
(iii) passivating the reductively calcined catalyst precursor from step (ii);
(iv) activating the passivated catalyst from step (iii).

2. The process according to claim 1 , wherein the catalytic or conventional support material is contacted with the soluble compounds of the active metals and optionally with the soluble compounds of the added catalyst elements by soaking or impregnation.

3. The process according to claim 1 , wherein the one or more active metals are selected from the group consisting of Co, Ru, Sn, Ni and Cu.

4. The process according to claim 1 , wherein one of the one or more active metals is Ru or Co.

5. The process according to claim 1 , wherein the soluble compounds of the active metals that are contacted with the support material are used partly or completely in the form of their nitrates or nitrosylnitrates.

6. The process according to claim 1 , wherein the support material comprises Al and/or Zr.

7. The process according to claim 1 , wherein the support material is contacted simultaneously or successively with a soluble Ru compound and a soluble Co compound, where the soluble cobalt compound is Co nitrate.

8. The process according to claim 1 , wherein the reactor in which the reductive calcination is conducted is a shaft reactor, rotary furnace, staged furnace or fluidized bed reactor.

9. The process according to claim 1 , wherein the temperature in the reductive calcination is in the range from 100 to 300° C.

10. The process according to claim 1 , wherein the reductive calcination is effected in a reactor connected to a denox plant.

11. The process according to claim 1 , that the temperature in the activation is in the range from 100 to 300° C.

12. The process according to claim 1 , wherein the reductive calcination is in the presence of hydrogen and an inert gas.

13. The process according to claim 12 , wherein hydrogen is present in an amount from 1 to 50% by volume.

14. The process according to claim 12 , wherein hydrogen is present in an amount from 2.5% to 30% by volume.

15. The process according to claim 12 , wherein hydrogen is present in an amount from 5% to 25% by volume.

16. The process according to claim 1 , wherein the catalyst precursor is prepared by coprecipitation and comprise the active metals Ru, Co and Sn.

17. The process according to claim 1 , wherein the catalyst precursor comprises:
0.01% to 20% by weight of catalytically active components of Ru, calculated as RuO;
1% to 50% by weight of catalytically active components of Co, calculated as CoO; and
0.1% to 5% by weight of catalytically active components of Sn, calculated as SnO.

18. The process according to claim 1 , wherein the catalyst precursor comprises:
1% to 10% by weight of catalytically active components of Ru, calculated as RuO;
20% to 40% by weight of catalytically active components of Co, calculated as CoO; and
1% to 3% by weight of catalytically active components of Sn, calculated as SnO.

19. A process for preparing alkanolamines and/or ethyleneamines in a liquid phase, by reacting ethylene glycol and/or monoethanolamine with ammonia in the presence of an amination catalyst comprising one or more active metals selected from Sn and the elements of groups 8, 9, 10 and 11 of the Periodic Table of the Elements, wherein the preparation of the amination catalyst comprises the following steps:
(i) preparing a catalyst precursor by contacting a conventional or catalytic support material with one or more soluble compounds of the active metals and optionally one or more soluble compounds of added catalyst elements;
(i)(a) optionally a work-up step comprising one or more of the steps of separation, washing and drying;
(ii) reductively calcining the catalyst precursor obtaining in step (i), where the reductive calcination is effected in the presence of hydrogen and the oxygen content in the reductive calcination is less than 0.1% by volume and the reductive calcination is at a temperature of 100 to 280° C.;
(iii) passivating the reductively calcined catalyst precursor from step (ii);
(iv) activating the passivated catalyst from step (iii),
with the proviso that an oxidation calcination is not carried out in the process.

20. The process according to claim 1 , which requires the work-up step comprising one or more of the steps of separation, washing and drying.

Assignees

• Basf Se

Inventors

• Bebensee Regine Helga
• Heidemann Thomas
• Becker Barbara
• Koch Eva
• Luyken Hermann
• Melder Johann-Peter

Classifications

• B01J21/02

  Boron or aluminium; Oxides or hydroxides thereof · CPC title

• C07C209/16 Primary

  with formation of amino groups bound to acyclic carbon atoms or to carbon atoms of rings other than six-membered aromatic rings · CPC title

• B01J23/75

  Cobalt · CPC title

• B01J21/066

  Zirconium or hafnium; Oxides or hydroxides thereof · CPC title

• B01J8/1872

  Details of the fluidised bed reactor (B01J8/1836 takes precedence) · CPC title