Purification of crude isophoronediamine by partial condensation in series with total condensation
The present invention is directed to a process for fine purification of isophoronediamine from the production of isophoronediamine wherein the crude isophoronediamine I is subjected to a fine purification by means of two vacuum distillation columns, wherein I. in the first vacuum distillation column K I low-boiling by-products still present are removed, and a crude IPDA II is transferred from the bottom of K I into the vacuum distillation column K II, II. and in the second vacuum distillation column K II the isophoronediamine is obtained in pure form overhead and separated from the organic residues, wherein the first condenser is a partial condenser and the pure IPDA is removed therein, and wherein the second condenser is a total condenser and the residual portion of the vapor stream from K II is completely condensed therein and recycled as return stream into the first vacuum distillation column K I.
1. A process for fine purification of isophoronediamine from the production of isophoronediamine by aminating hydrogenation of isophorone nitrile in the presence of at least ammonia, hydrogen, a hydrogenation catalyst and optionally further additions and in the presence or absence of organic solvents to obtain a crude isophoronediamine I,
wherein the crude isophoronediamine I is subjected to a fine purification by means of two vacuum distillation columns, wherein
I. in the first vacuum distillation column K I low-boiling by-products still present are removed, and a crude IPDA II is transferred from the bottom of K I into the vacuum distillation column K II,
II. and in the second vacuum distillation column K II the isophoronediamine is obtained in pure form overhead and separated from the organic residues, with two condensers being mounted at the top of the second vacuum distillation column,
wherein the first condenser is a partial condenser and the pure IPDA is removed therein,
and wherein the second condenser is a total condenser and the residual portion of the vapour stream from K II is completely condensed therein and recycled as return stream into the first vacuum distillation column K I.
2. The process according to claim 1 , wherein the crude isophoronediamine I has the following composition:
IPDA 75-100 wt %
Water 0-15 wt %
Low boilers 0-6 wt %
High boilers 0-6 wt %
Residual ammonia 10-1000 ppm.
3. The process according to claim 1 , wherein the first vacuum distillation column K I has the following parameters:
Temperature 40-120° C.
Pressure 10-200 mbar
Theoretical plates 10-80.
4. The process according to claim 1 , wherein the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm.
5. The process according to claim 1 , wherein the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50.
6. The process according to claim 1 , wherein the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
7. The process according to claim 1 , wherein the crude isophoronediamine I has the following composition:
IPDA 75-100 wt %
Water 0-15 wt %
Low boilers 0-6 wt %
High boilers 0-6 wt %
Residual ammonia 10-1000 ppm,
and
in that the first vacuum distillation column K I has the following parameters:
Temperature 40-120° C.
Pressure 10-200 mbar
Theoretical plates 10-80
and
in that the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm,
and
in that the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50
and
in that the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
8. The process according to claim 1 , wherein the purity of the pure isophoronediamine is at least 98% by weight and the residual ammonia content in the pure IPDA is less than 50 ppm.
9. The process according to claim 2 , wherein the first vacuum distillation column K I has the following parameters:
Temperature 40-120° C.
Pressure 10-200 mbar
Theoretical plates 10-80.
10. The process according to claim 2 , wherein the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm.
11. The process according to claim 2 , wherein the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50.
12. The process according to claim 2 , wherein the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
13. The process according to claim 2 , wherein the crude isophoronediamine I has the following composition:
IPDA 75-100 wt %
Water 0-15 wt %
Low boilers 0-6 wt %
High boilers 0-6 wt %
Residual ammonia 10-1000 ppm,
and
in that the first vacuum distillation column K I has the following parameters:
Temperature 40-120° C.
Pressure 10-200 mbar
Theoretical plates 10-80
and
in that the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm,
and
in that the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50
and
in that the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
14. The process according to claim 2 , wherein the purity of the pure isophoronediamine is at least 98% by weight and the residual ammonia content in the pure IPDA is less than 50 ppm.
15. The process according to claim 3 , wherein the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm.
16. The process according to claim 3 , wherein the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50.
17. The process according to claim 3 , wherein the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
18. The process according to claim 3 , wherein the crude isophoronediamine I has the following composition:
IPDA 75-100 wt %
Water 0-15 wt %
Low boilers 0-6 wt %
High boilers 0-6 wt %
Residual ammonia 10-1000 ppm,
and
in that the first vacuum distillation column K I has the following parameters:
Temperature 40-120° C.
Pressure 10-200 mbar
Theoretical plates 10-80
and
in that the composition of the feed stream crude IPDA II from the first vacuum distillation column into the second vacuum distillation column has the following composition:
IPDA 90-100 wt %
High boilers 0-10 wt %
Residual ammonia 10-500 ppm, and
in that the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50
and
in that the partial condenser used at the top of the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Temperature 80-200° C.
19. The process according to claim 3 , wherein the purity of the pure isophoronediamine is at least 98% by weight and the residual ammonia content in the pure IPDA is less than 50 ppm.
20. The process according to claim 4 , wherein the second vacuum distillation column K II has the following parameters:
Pressure 10-200 mbar
Tops temperature 80-200° C.
Theoretical plates 5-50.