Process for the energy-efficient production of alkali metal alkoxides

Patent metadata

Field	Value
Publication number	US-12180141-B2
Application number	US-202217659086-A
Country	US
Kind code	B2
Filing date	Apr 13, 2022
Priority date	Apr 16, 2021
Publication date	Dec 31, 2024
Grant date	Dec 31, 2024

Abstract

A process produces sodium and/or potassium alkoxides in countercurrent by reactive rectification. Alcohol is reacted in countercurrent with the respective alkali metal hydroxide. The vapours containing alcohol and water are separated in at least two serially arranged rectification columns. The energy of the vapour obtained in the second rectification is utilized for operating the first rectification. This specific energy integration coupled with establishing a certain pressure difference in the two rectification stages makes it possible to cover a particularly large proportion of the energy required for the rectification through heating steam and minimizes the use of electricity.

First claim

The invention claimed is:

1. A process for producing at least one alkali metal alkoxide of formula M A OR, wherein R is a C 1 to C 6 hydrocarbon radical, and wherein M A is sodium or potassium, the process comprising:
(a1) reacting a reactant stream S AE1 comprising ROH with a reactant stream S AE2 comprising M A OH, in countercurrent at a pressure p 3A and a temperature T 3A in a first reactive rectification column RR A , to afford a crude product RP A comprising M A OR, water, the ROH, and the M A OH, wherein R is a C 1 to C 5 hydrocarbon radical, and M A is sodium or potassium, and
withdrawing a bottoms product stream S AP comprising the ROH and the M A OR at a lower end of the first reactive rectification column RR A , and withdrawing a vapour stream S AB comprising the water and the ROH at an upper end of the first reactive rectification column RR A , and
(a2) optionally, simultaneously with and spatially separate from (a1), reacting a reactant stream S BE1 comprising ROH with a reactant stream S BE2 comprising M B OH, in countercurrent at a pressure pam and a temperature T 3B in a second reactive rectification column RR B , to afford a crude product RP B comprising M B OR, water, the ROH, and the M B OH, wherein M B is sodium or potassium, and
withdrawing a bottoms product stream S BP comprising the ROH and the M B OR at a lower end of the second reactive rectification column RR B , and withdrawing a vapour stream S BB comprising the water and the ROH at an upper end of the second reactive rectification column RR B ,
(b) passing the vapour stream S AB into a first rectification column RD 1 , and, if (a2) is performed, the vapour stream S BB is also passed into the first rectification column RD 1 in admixture with the vapour stream S AB or separately from the vapour stream S AB , to obtain a mixture G RD1 comprising water and ROH in the first rectification column RD 1 ,
(c) separating the mixture G RD1 or the vapour stream S AB in the first rectification column RD 1 at a pressure p 1 and a temperature T 1 , into an ROH-comprising vapour stream S RDB1 at an upper end of the first rectification column RD 1 , and a bottoms stream S RDS1 comprising water and ROH at a lower end of the first rectification column RD 1 ,
(d) passing the bottoms stream S RDS1 completely or partially into a second rectification column RD 2 , to obtain a mixture G RD2 comprising water and ROH in the second rectification column RD 2 ,
(e) separating the mixture G RD2 at a pressure p 2 and a temperature T 2 , into an ROH-comprising vapour stream S RDB2 at a top of the second rectification column RD 2 , and a bottoms stream S RDS2 comprising water at a lower end of the second rectification column RD 2 , and
(f) transferring energy from the vapour stream S RDB2 to the mixture G RD1 or to the vapour stream S AB in the first rectification column RD 1 ,
wherein p 2 >p 1 , p 2 >p 3A , and wherein if (a2) is performed, p 2 >p 3B .

2. The process according to claim 1 , wherein in (f), energy is directly transferred from the vapour stream S RDB2 to the mixture G RD1 or to the vapour stream S AB .

3. The process according to claim 2 , wherein at least one of (α-i), (α-ii), and/or (α-iii) is performed:
(α-i) a first portion S RDS11 of the bottoms stream S RDS1 discharged from the first rectification column RD 1 is passed into the second rectification column RD 2 , and energy is transferred from the vapour stream S RDB2 to a second portion S RDS12 of the bottoms stream S RDS1 discharged from the first rectification column RD 1 , and the second portion S RDS12 is then recycled into the first rectification column RD 1 ;
(α-ii) at least one stream S RDX1 , distinct from the vapour stream S RDB1 and the bottoms stream S RDS1 , comprising ROH and water is discharged from the first rectification column RD 1 , and energy is then transferred from the vapour stream S RDB2 to the at least one stream S RDX1 , and the at least one stream S RDX1 is recycled into the first rectification column RD 1 ; and/or
(α-iii) the vapour stream S RDB2 is passed through the first rectification column RD 1 , thus transferring energy from the vapour stream S RDB2 to the mixture G RD1 or to the vapour stream S AB .

4. The process according to claim 1 , wherein in (f), energy is indirectly transferred from the vapour stream S RDB2 to the mixture G RD1 or to the vapour stream S AB .

5. The process according to claim 4 , wherein at least one of (β-i), (β-ii), and/or (β-iii) is performed:
(β-i) a first portion S RDS11 of the bottoms stream S RDB1 discharged from the first rectification column RD 1 is passed into the second rectification column RD 2 , and a second portion S RDS12 of the bottoms stream S RDS1 discharged from the first rectification column RD 1 is recycled into the first rectification column RD 1 , wherein energy is transferred from the vapour stream S RDB2 to at least one heat transfer medium W i1 , distinct from the second portion S RDS12 , and is then transferred from the at least one heat transfer medium W i1 to the second portion S RDS12 , and the second portion S RDS12 is then recycled into the first rectification column RD 1 ;
(β-ii) at least one stream S RDX1 , distinct from the vapour stream S RDB1 and the bottoms stream S RDS1 , comprising ROH and water is discharged from the first rectification column RD 1 , and energy is transferred from the vapour stream S RDB2 to at least one heat transfer medium W ii1 , distinct from the at least one stream S RDX1 , and then transferred from the at least one heat transfer medium W ii1 to the at least one stream S RDX1 , and the at least one stream S RDX1 is then recycled into the first rectification column RD 1 ; and/or
(β-iii) energy is transferred from the vapour stream S RDB2 to at least one heat transfer medium W iii1 , distinct from the mixture G RD1 or the vapour stream S AB , and the at least one heat transfer medium Win, is then passed through the first rectification column RD 1 , thus transferring energy from the at least one heat transfer medium W iii1 to the mixture G RD1 or to the vapour stream S AB .

6. The process according to claim 5 , wherein each of the at least one heat transfer medium W i1 , the at least one heat transfer medium W ii1 , and the at least one heat transfer medium W iii1 is water.

7. The process according to claim 5 , wherein the at least one stream S RDX1 is withdrawn below the vapour stream S RDB1 on the first rectification column RD 1 .

8. The process according to claim 1 , wherein the vapour stream S RDB2 is at least partially employed as the reactant stream S AE1 in the first reactive rectification column RR A , and, if (a2) Is performed, the vapour stream S RDB2 is alternatively or in addition employed as the reactant stream S BE1 in the second reactive rectification column RR B .

9. The process according to claim 1 , wherein the vapour stream S RDB1 is at least partially employed as the reactant stream S AE1 in the first reactive rectification column RR A , and, if (a2) is performed, the vapour stream S RDB1 is alternatively or in addition employed as the reactant stream S BE1 in the second reactive rectification column RR B .

10. The process according to claim 1 , wherein a stream S XE1 , distinct from the reactant stream S AE1 and the reactant stream S BE1 comprising ROH is added to at least one of the columns selected from the group consisting of the first rectification column RD 1 , the second rectification column RD 2 , and the first reactive rectification column RR A , and, if (a2) is performed, the stream S XE1 is alternatively or in addition added to the second reactive rectification colum

Assignees

• Evonik Operations Gmbh

Inventors

• Roettger Dirk
• Reimann Sebastian
• Paul Niklas
• Rix Armin Matthias
• Schröder Moritz
• Zitzewitz Philip

Classifications

• C07B63/00

  Purification; Separation (separation of optically-active compounds C07B57/00); Stabilisation; Use of additives · CPC title

• Y02P20/10

  Process efficiency · CPC title

• C07C29/80 Primary

  by distillation · CPC title

• C07C29/70 Primary

  by converting hydroxy groups to O-metal groups {(C07C29/09 takes precedence)} · CPC title

• C07C31/04

  Methanol · CPC title