Process and catalyst for preparing 1,4-butanediol

Patent metadata

Field	Value
Publication number	US-2019232256-A1
Application number	US-201716338015-A
Country	US
Kind code	A1
Filing date	Sep 27, 2017
Priority date	Sep 30, 2016
Publication date	Aug 1, 2019
Grant date	—

Abstract

The present invention relates to a process for preparing 1,4-butanediol (BDO) by hydrogenating 2-butyne-1,4-diol (BYD) or 4-hydroxybutanal (4-HBA) in the presence of a catalyst of the Raney type having a porous foam structure, wherein the macroscopic pores have sizes in the range of 100 to 5000 μm, and a bulk density of up to 0.8 kg/L.

First claim

1 - 17 . (canceled)

18 . A process for preparing 1,4-butanediol by hydrogenating 2-butyne-1,4-diol or 4-hydroxybutanal, wherein an aqueous solution comprising 2-butyne-1,4-diol or 4-hydroxybutanal is brought into contact with hydrogen and an activated nickel catalyst having a porous foam structure, wherein the macroscopic pores have sizes in the range of 100 to 5000 μm, and a bulk density of not more than 0.8 kg/L.

19 . The process of claim 18 , wherein the hydrogenation of 4-hydroxybutanal is carried out at a hydrogen pressure in the range of 10 to 110 bar.

20 . The process of claim 19 , wherein the hydrogenation is carried out in a temperature range of 50 to 200° C.

21 . The process of claim 18 , wherein the hydrogenation of butyne-1,4-diol is carried out at a hydrogen pressure in the range of 50 to 350 bar.

22 . The process of claim 21 , wherein the hydrogenation is carried out in a temperature range of 50 to 150° C.

23 . The process of claim 21 , wherein the hydrogenation is carried out continuously, wherein the catalyst is present as a fixed bed in a reactor operated adiabatically, the temperature in the reactor inlet is in the range of 80 to 100° C. and the temperature in the reactor outlet is in the range of 110 to 150° C.

24 . The process of claim 21 , wherein the hydrogenation is carried out batchwise in a stirred tank reactor, wherein the catalyst is arranged in a holding device close to the stirrer shaft such that a flow of the reaction mixture through the catalyst bed is generated by the stirrer.

25 . The process of claim 24 , wherein the temperature in the stirred tank at the start of the reaction is maintained in a range of 90 to 105° C. such that butyne-1,4-diol is reacted with hydrogen at least partially to give butene-1,4-diol and the temperature is then increased to 130 to 135° C. and maintained until completion of the hydrogenation to give 1,4-butanediol.

26 . The process of claim 18 , wherein the activated nickel catalyst has an aluminium content of not more than 15% by weight.

27 . The process of claim 26 , wherein the activated nickel catalyst has a porous foam structure, wherein the macroscopic pores have sizes in the range of 200 to 2500 μm.

28 . The process of claim 18 , wherein the activated nickel catalyst comprises 0 to 10% by weight of at least one of the elements selected from the group consisting of molybdenum, iron and chromium.

29 . An activated nickel catalyst having a porous foam structure, wherein the macroscopic pores have sizes in the range of 100 to 5000 μm, and a bulk density of not more than 0.8 kg/L.

30 . The activated nickel catalyst of claim 29 , wherein the catalyst has an average particle size of at most 70 mm.

31 . The activated nickel catalyst of claim 29 , wherein the catalyst is present as loose material of cuboidal particles with edge lengths of not more than 50 mm.

32 . The activated nickel catalyst of claim 29 , wherein the catalyst has an aluminium content of not more than 15% by weight.

33 . The activated nickel catalyst of claim 29 , wherein the catalyst has a porous foam structure, wherein the macroscopic pores have sizes in the range of 200 to 2500 μm.

34 . The activated nickel catalyst of claim 29 , wherein the catalyst comprises 0.05 to 10% by weight of at least one of the elements selected from the group consisting of molybdenum, iron and chromium.

35 . The process of claim 22 , wherein the hydrogenation is carried out continuously, wherein the catalyst is present as a fixed bed in a reactor operated adiabatically and the temperature in the reactor inlet is in the range of 80 to 100° C. and the temperature in the reactor outlet is in the range of 110 to 150° C.

36 . The process of claim 35 , wherein the activated nickel catalyst has an aluminium content of not more than 15% by weight.

37 . The process of claim 36 , wherein the activated nickel catalyst has a porous foam structure, wherein the macroscopic pores have sizes in the range of 200 to 2500 μm.

Assignees

• Evonik Degussa Gmbh

Inventors

• Berweiler Monika
• Göttlinger Markus
• Roos Meike
• Schwarz Matthias
• Poss René

Classifications

• C07C29/172

  with the obtention of a fully saturated alcohol · CPC title

• B01J37/0217

  Pretreatment of the substrate before coating · CPC title

• B01J23/755

  Nickel · CPC title

• B01J23/28

  Molybdenum · CPC title

• B01J37/0215

  Coating · CPC title