Urea production process and plant

Patent metadata

Field	Value
Publication number	US-10759745-B2
Application number	US-201816186410-A
Country	US
Kind code	B2
Filing date	Nov 9, 2018
Priority date	Nov 10, 2017
Publication date	Sep 1, 2020
Grant date	Sep 1, 2020

Abstract

Processes and plants for the production of purified urea solution are described. In a described urea production process, urea is produced in a synthesis section without a high pressure stripper and the urea solution is subjected to purification after the recovery section, to give purified urea solution and off-gas. The purification comprises e.g. steam stripping.

First claim

The invention claimed is:

1. A process for the production of a purified urea solution optionally after dilution, the process comprising:
A) reacting CO 2 and NH 3 under urea synthesis conditions in a urea synthesis reactor operating at high pressure, to give a urea synthesis stream containing urea, NH 3 , CO 2 and an amount of ammonium carbamate,
B) expanding the urea synthesis stream in a recovery section thereby reducing the pressure, wherein the urea synthesis stream that is expanded comprises at least 90 wt. % of said amount of ammonium carbamate,
and heating at least part of the expanded urea synthesis stream in one or more dissociation units at medium and/or low pressure, to give an aqueous urea stream and a recovery section vapour containing NH 3 and CO 2 ,
C) subjecting in a purification section at least part of the aqueous urea stream to purification, wherein the purification is stripping to remove ammonia and/or wherein the purification yields a urea solution with an alkalinity as NH 3 of less than 0.2 wt. % when the alkalinity is converted on the basis of water added or removed as necessary to have 32.5 wt. % urea, giving a purified urea solution and a purification section off-gas containing water and ammonia,
D) optionally diluting at least part of i) the purified urea solution from step C) and/or ii) the aqueous urea stream from step B) prior to the stream's purification in step C), with water to obtain a target concentration of urea in said solution and/or stream,
E) wherein the purification section comprises a purification section condenser and the purification section off-gas is condensed in the purification section condenser to give purification section condensate and said purification section condensate is recycled to said urea synthesis reactor.

2. A process according to claim 1 , wherein the purification section condensate is supplied by liquid flow to the urea synthesis reactor, and wherein the purification is low pressure steam stripping and involves contacting the aqueous urea stream in counter current flow with steam at a pressure of less than 3 bar.

3. A process according to claim 1 , further comprising:
(a) condensing the recovery section vapour to give a liquid ammonium carbamate recycle stream in a recovery section condenser, wherein said condenser operates at a lower pressure than said urea synthesis reactor,
(b) supplying the ammonium carbamate recycle stream to the urea synthesis reactor,
(c) and supplying said purification section condensate to said recovery section condenser before said purification section condensate is recycled to said urea synthesis reactor in step E.

4. A process according to claim 3 , further comprising a step of supplying non-condensed gases from the recovery section condenser, to a scrubbing step with a scrubbing liquid in a scrubber to give a scrubbed gas and a spent scrubbing liquid, and wherein the purification section condenser gives a second off-gas and the process further comprises supplying the second off-gas from the purification section condenser to said scrubber.

5. A process according to claim 1 , wherein step B comprises
B 1 ) expanding the urea synthesis stream to medium pressure, and heating at least part of the urea synthesis stream at medium pressure to give a MP recovery section vapour and a MP aqueous urea solution, and
B 2 ) expanding the MP aqueous urea solution to low pressure, and heating the expanded aqueous urea stream at low pressure to give a LP recovery section vapour and a LP aqueous urea solution.

6. A process according to claim 1 , wherein step A involves supplying a fresh CO 2 feed into the reactor, wherein at least 85% of the fresh CO 2 feed is added directly into the reactor.

7. A process according to claim 1 , wherein said step C further comprises expanding said aqueous urea stream, to the operating pressure of the purification section to provide an expanded aqueous urea stream, and wherein step C comprises steam stripping the expanded aqueous urea stream, wherein the steam stripping involves direct injection of steam in the expanded aqueous urea stream.

8. A process according to claim 7 , wherein the steam stripping is carried out at 0.010 to 1.5 bar absolute in a stripping column with a cyclone separator at the top of the column, a liquid distribution tray and a packed bed, wherein gas is separated from the expanded aqueous urea stream in the cyclone separator, the gas exits through an outlet at the top, liquid flows down from the cyclone separator onto the liquid distribution tray, and the liquid distribution tray distributes the liquid over the packed bed.

9. A process according to claim 1 , wherein no passivation air is used.

10. The process according to claim 1 , wherein the purified urea solution is suitable for use in NOx abatement.

11. The process according to claim 1 , wherein the purified urea solution is suitable for use as diesel exhaust fluid (DEF) optionally after dilution.

12. The process according to claim 7 , wherein the purification section operating pressure is in the range of 0.010 to 1.5 bar absolute.

13. A process according to claim 1 , wherein step A involves supplying a CO 2 feed into the reactor and wherein the CO 2 feed contains less than 0.05 wt. % oxygen.

14. The process according to claim 1 , wherein the high pressure is a pressure between 120 and 300 bar.

15. The process according to claim 1 , wherein the medium pressure is a pressure between 10 and 70 bar.

16. The process according to claim 15 , wherein the medium pressure is a pressure between 15 and 25 bar.

17. The process according to claim 1 , wherein the low pressure is a pressure between 0 and 10 bar.

18. The process according to claim 17 , wherein the low pressure is a pressure between 3 and 5 bar.

Assignees

• Stamicarbon

Inventors

• Pustjens Ronny Albert Mathijs
• Van Den Tillaart Johan Albert Arno

Classifications

• Y02A50/20

  Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters · CPC title

• Y02T10/12

  Improving ICE efficiencies · CPC title

• B01J2219/0286

  Steel · CPC title

• C07C273/04 Primary

  from carbon dioxide and ammonia · CPC title

• B01D5/0057

  in combination with other processes · CPC title