Process for extracting sulphur-containing compounds by liquid-liquid extraction by means of a soda solution with an optimized final washing step

Patent metadata

Field	Value
Publication number	US-9512367-B2
Application number	US-201214360385-A
Country	US
Kind code	B2
Filing date	Oct 16, 2012
Priority date	Nov 24, 2011
Publication date	Dec 6, 2016
Grant date	Dec 6, 2016

Abstract

Process of extracting sulphur-containing compounds from a hydrocarbon cut of the gasoline or LPG type by liquid-liquid extraction with a soda solution employing a unit ( 2 ) for pretreatment of the feedstock to be treated placed upstream of the extraction unit ( 4 ), the soda being introduced into the extraction column ( 4 ) in the form of two circuits operating either in parallel, or in series.

First claim

The invention claimed is:

1. A process of extracting sulphur-containing compounds from a hydrocarbon cut of gasoline or LPG comprising:
subjecting said hydrocarbon cut to liquid-liquid extraction with a soda solution, implemented in a pretreatment unit ( 2 ) for pretreatment of said hydrocarbon cut, and further subjecting said hydrocarbon cut to liquid-liquid extraction with a soda solution in an extraction column ( 4 ) having a top and a bottom, wherein said pretreatment unit ( 2 ) is positioned upstream of said extraction column ( 4 ), and wherein soda solution is introduced into said extraction column ( 4 ) via a first circuit and a second circuit that function as follows:
said first circuit removes used soda solution from the bottom of said extraction column ( 4 ) at a point of withdrawal and introduces said used soda solution into a first oxidation reactor ( 9 ) and then into a first separating vessel ( 12 ) for separating the soda solution resulting in the production of a partially regenerated soda solution ( 6 ),
a first part ( 6 ′) of said partially regenerated soda solution is then introduced at an intermediate point of said extraction column ( 4 ) so as to separate said column into an upper compartment situated between said intermediate point and an upper end of said extraction column ( 4 ), and a lower compartment situated between said intermediate point and said point of withdrawal of used soda solution ( 7 ) at the bottom of said extraction column ( 4 ), and
said second circuit introduces a clean soda solution ( 16 ) at the top of said extraction column ( 4 ) via a feed pipe, withdraws soda solution ( 17 ) from said upper compartment, and then returns the soda solution ( 17 ) to said feed pipe for clean soda solution ( 16 ),

wherein the ratio R 2 of the flow rate of soda solution ( 17 ) removed from said upper compartment of said extraction column ( 4 ) to the flow rate of clean soda ( 16 ) solution introduced at the top of said extraction column ( 4 ) is between 1.0 and 10.

2. The process according to claim 1 , wherein the upper part of said extraction column ( 4 ) functions as a single theoretical stage of extraction and the lower compartment of said extraction column 4 functions as a set of N theoretical stages in series wherein N is between 1 and 4.

3. The process according to claim 1 , wherein said partially regenerated soda solution ( 6 ) from said first separating vessel ( 12 ) is split into said first part ( 6 ′) of said partially regenerated soda solution and a second part ( 24 ) of said partially regenerated soda solution, and said second part ( 24 ) of said partially regenerated soda solution is sent to a second oxidation reactor ( 25 ), then to a second separating vessel ( 18 ), and then to a third separating vessel ( 19 ), and clean soda solution ( 16 ) is removed from said third separating vessel ( 19 ) and sent to said feed pipe for introducing clean soda solution ( 16 ) at the top of said extraction column ( 4 ).

4. The process according to claim 3 , wherein the ratio R 1 of the flow rate of said second part of partially regenerated soda solution ( 24 ) entering said second oxidation reactor ( 25 ) to the flow rate of partially regenerated soda ( 6 ) removed from said first separating vessel ( 12 ) is between 0.01 and 0.25.

5. The process according to claim 3 , wherein the ratio R 1 of the flow rate of said second part of partially regenerated soda solution ( 24 ) entering said second oxidation reactor ( 25 ) to the flow rate of partially regenerated soda ( 6 ) removed from said first separating vessel ( 12 ) is between 0.05 and 0.15.

6. The process according to claim 3 , wherein the ratio R 2 of the flow rate of soda solution ( 17 ) removed from said upper compartment of said extraction column ( 4 ) to the flow rate of clean soda solution ( 16 ) introduced at the top of said extraction column ( 4 ) is between 1 and 5.

7. The process according to claim 4 , wherein the ratio R 2 of the flow rate of soda solution ( 17 ) removed from said upper compartment of said extraction column ( 4 ) to the flow rate of clean soda solution ( 16 ) introduced at the top of said extraction column ( 4 ) is between 1 and 5.

8. The process according to claim 5 , wherein the ratio R 2 of the flow rate of soda solution ( 17 ) removed from said upper compartment of said extraction column ( 4 ) to the flow rate of clean soda solution ( 16 ) introduced at the top of said extraction column ( 4 ) is between 1 and 5.

9. The process according to claim 3 , wherein the flow rate of said second part of partially regenerated soda solution ( 24 ) represents from 1 to 25% by weight of the flow rate of partially regenerated soda ( 6 ) removed from said first separating vessel ( 12 ).

10. The process according to claim 3 , wherein the flow rate of said second part of partially regenerated soda solution ( 24 ) represents from 5% to 15% by weight of the flow rate of partially regenerated soda ( 6 ) removed from said first separating vessel ( 12 ).

11. The process according to claim 1 , wherein a flow ( 10 ′) of hydrocarbon is injected into the used soda solution upstream of said first separating vessel ( 12 ) to extract disulfides and to recover soda solution by decanting in said first separating vessel ( 12 ).

12. The process according to claim 1 , wherein air ( 8 ) is introduced into said oxidation reactor ( 9 ) to promote oxidation of the sodium thiolates to disulfides.

13. The process according to claim 11 , wherein air ( 8 ) is introduced into said oxidation reactor ( 9 ) to promote oxidation of the sodium thiolates to disulfides.

14. The process according to claim 3 , wherein
air ( 8 ) is introduced into said oxidation reactor ( 9 ) to promote oxidation of the sodium thiolates to disulfides,
a flow ( 10 ) of hydrocarbon is injected into said second part of partially regenerated soda solution ( 24 ) upstream of said said second oxidation reactor ( 25 ) to extract disulfides, and
air ( 23 ) is introduced into second oxidation reactor ( 25 ) to convert residual sodium thiolates to disulfides.

15. The process according to claim 1 , wherein the upper part of said extraction column ( 4 ) functions as a single theoretical stage of extraction and the lower compartment of said extraction column 4 functions as a set of N theoretical stages in series wherein N is between 1 and 2.

Assignees

• Ifp Energies Now

Inventors

• Augier Frederic
• Baudot Arnaud
• Gazarian Jeremy
• Leinekugel Le Cocq Damien

Classifications

• C10G21/30 Primary

  Controlling or regulating · CPC title

• C10G19/02 Primary

  with aqueous alkaline solutions · CPC title

• C10G21/08

  Inorganic compounds only · CPC title

• C10G21/28 Primary

  Recovery of used solvent · CPC title