Method for operating a gas-phase phosgenation plant

Patent metadata

Field	Value
Publication number	US-9840461-B2
Application number	US-201515128179-A
Country	US
Kind code	B2
Filing date	Mar 24, 2015
Priority date	Mar 27, 2014
Publication date	Dec 12, 2017
Grant date	Dec 12, 2017

Abstract

This invention relates to a process for operating a gas phase phosgenation plant ( 100 ) to form an isocyanate ( 4 ) by reacting an amine ( 2 ) with phosgene ( 1 ), in which the gas phase phosgenation plant is started up by first charging the plant with phosgene. At the same time as, or after the first charge of phosgene, the amine supply devices are rendered inert using a hot inert gas stream ( 30 ). Then, amine is admixed for the first time. In this way and by maintaining a pressure drop in the amine and phosgene devices to the mixing zone, the back mixing of phosgene into the amine-containing reactant stream during start-up is prevented.

First claim

The invention claimed is:

1. A method of operating a gas phase phosgenation plant that is configured to produce an isocyanate ( 4 ) by reacting an amine with phosgene and that comprises at least
(i) an apparatus for providing a gaseous phosgene stream,
(ii) an apparatus for providing a gaseous amine stream,
(iii) a mixing zone for mixing the gaseous phosgene stream and the gaseous amine stream, with the mixing zone being connected by connecting devices for the phosgene stream and for the amine stream to the apparatus for providing a gaseous phosgene stream and the apparatus for providing a gaseous amine stream,
(iv) a reaction zone arranged downstream of the mixing zone for further conversion of the previously mixed streams,
(v) a reaction stopping zone arranged downstream of the reaction zone to end the reaction,
and optionally
(vi) a workup section which comprises devices for recovery and recycling of unconverted phosgene and devices for obtaining the isocyanate prepared in pure form,
wherein the gas phase phosgenation plant is started up by:
(I) providing a gaseous phosgene stream at a temperature T 10 of 200° C. to 600° C. with an absolute pressure p 10 of 100 mbar to 3000 mbar in the apparatus for providing a gaseous phosgene stream and continuously introducing this gaseous phosgene stream through the connecting device for the phosgene stream into the mixing zone, the reaction zone and the reaction stopping zone, the pressure p 10 being greater than the pressure p 3100 in the mixing zone;
(II) either simultaneously with or after step (I),
(a) introducing an inert substance, at a temperature T 3 <200° C. into the apparatus for providing a gaseous amine stream, heating the inert substance in the apparatus for providing a gaseous amine stream to obtain an inert gas stream and passing said inert gas stream through the connecting device for the amine stream, the mixing zone, the reaction zone and the reaction stopping zone
or
(b) introducing an inert gas stream
(b.1) into the connecting device for the amine stream and thence through the mixing zone, the reaction zone and the reaction stopping zone
or
(b.2) into the apparatus for providing a gaseous amine stream and thence through the connecting device for the amine stream, the mixing zone, the reaction zone and the reaction stopping zone,
where the inert gas stream in variant (a) and in variant (b) has a temperature of 200° C. to 600° C. and an absolute pressure p 30 of 100 mbar to 3000 mbar,
and
where the pressure p 30 in variant (a) and in variant (b) is greater than the pressure p 3100 in the mixing zone;

and
(III) after (II), providing a gaseous amine stream at a temperature T 20 of 200° C. to 600° C. with an absolute pressure p 20 of 100 mbar to 3000 mbar in the apparatus for providing a gaseous amine stream and continuously introducing this gaseous amine stream through the connecting device for the amine stream into the mixing zone, where the pressure p 20 is greater than the pressure p 3100 in the mixing zone, and where the composition and the mass flow rate of the gaseous amine stream are matched to the composition and the mass flow rate of the gaseous phosgene stream such that, in the mixing zone, phosgene is present in a stoichiometric excess in relation to the primary amino groups of the amine.

2. The method as claimed in claim 1 , in which the gas phase phosgenation plant includes the workup section and in which, in the regular operation of the gas phase phosgenation plant, the phosgene in the phosgene gas stream comprises a mixture of fresh phosgene and recycled phosgene recovered in the recovery and recycling devices.

3. The method as claimed in claim 1 , in which the phosgene in the phosgene gas stream from (I) consists at least partly of recycled phosgene.

4. The method as claimed in claim 1 , in which the compositions and mass flow rates of streams of gaseous phosgene and of gaseous amine are matched to one another such that, in (III), in the mixing zone, phosgene is present in a stoichiometric excess in relation to the primary amino groups of the amine in an amount that is at least 150% of the theoretically required amount.

5. The method as claimed in claim 1 , in which the pressures p 10 and p 20 are the same.

6. The method as claimed in claim 1 , in which the mass flow rate of gaseous amine stream is increased continuously or in stages, to a desired target value M′ target .

7. The method as claimed in claim 6 , in which the mass flow rate of gaseous amine stream is increased such that at least 80% of the desired target value M′ target is attained within not more than 12 hours.

8. The method as claimed in claim 1 , in which the absolute pressure p 3100 is adjusted to a value of 80 mbar to 2500 mbar.

9. The method as claimed in claim 1 , in which the connecting device for the phosgene stream comprises a nozzle.

10. The method as claimed in claim 1 , in which the connecting device for the amine stream comprises a nozzle.

11. The method as claimed in claim 1 , in which the connecting devices for the phosgene stream and for the amine stream comprise a common nozzle apparatus.

12. The method as claimed in claim 1 , in which the inert gas stream is maintained during the performance of (III).

13. The method as claimed in claim 1 , in which the reaction stopping zone is operated below the boiling temperature of the isocyanate and above the breakdown temperature of the carbamoyl chloride which corresponds to the amine by contacting the gaseous process product exiting from the reaction zone with an inert solvent.

14. The method as claimed in claim 13 , in which the reaction stopping zone is put into operation no later than when the gaseous amine stream enters the mixing zone for the first time in (III).

15. The method as claimed in claim 1 , in which the amine is selected from the group consisting of isophoronediamine, hexamethylenediamine, bis(p-aminocyclohexyl)methane, tolylenediamine and diphenylmethanediamine.

16. The method as claimed in claim 1 , in which said inert substance introduced in (II) (a) is liquid at room temperature and standard pressure.

Assignees

• Covestro Deutschland Ag

Inventors

• Knauf Thomas
• Lorenz Wolfgang
• Steffens Friedhelm
• Bruns Rainer
• Taube Wolfgang

Classifications

• C07C263/20

  Separation; Purification · CPC title

• C07C263/10 Primary

  by reaction of amines with carbonyl halides, e.g. with phosgene · CPC title

• B01J12/005

  carried out at high temperatures, e.g. by pyrolysis · CPC title

• C01B32/80

  Phosgene · CPC title

• C01B31/28

  Chemistry & Metallurgy · mapped topic