PROCESS FOR SULFONE CONVERSION BY SUPER ELECTRON DONORS

• US 20130015104A1
• Filed: 07/12/2011
• Published: 01/17/2013
• Est. Priority Date: 07/12/2011
• Status: Abandoned Application

• Current Assignee: Saudi Arabian Oil Company (Government of Saudi Arabia)
• Original Assignee: Saudi Arabian Oil Company (Government of Saudi Arabia)
• Inventors: Al-Hajji, Adnan, Bourane, Abdennour, Koseoglu, Omer Refa
• Application Number:
  US13/181,043
• Publication Number:
  US 20130015104A1
• Time in Patent Office: Days
• US Class Current: 208/236
• CPC Class Codes: C10G 17/04 Liquid-liquid treatment forming two immiscible phases
• CPC Class Codes: C10G 2300/1037 Hydrocarbon fractions
• CPC Class Codes: C10G 2300/202 Heteroatoms content, i.e. S, N, O, P
• CPC Class Codes: C10G 2300/301 Boiling range
• CPC Class Codes: C10G 2300/4006 Temperature
• CPC Class Codes: C10G 2300/4012 Pressure
• CPC Class Codes: C10G 2300/4018 Spatial velocity, e.g. LHSV, WHSV
• CPC Class Codes: C10G 2300/44 Solvents
• CPC Class Codes: C10G 27/04 with oxygen or compounds generating oxygen
• CPC Class Codes: C10G 53/14 including at least one oxidation step

Abstract

A process wherein an electron donor agent is provided for the decomposition of sulfones and sulfoxides formed after the oxidative desulfurization of a sulfur-containing hydrocarbon stream.

Claims

1. A method of upgrading a hydrocarbon feedstock by removal of sulfones and sulfoxides therefrom, which comprises the steps of

a. supplying a hydrocarbon feedstock to an oxidation reactor, the hydrocarbon feedstock comprising sulfur-containing compounds;

b. contacting the hydrocarbon feedstock with an oxidant in the presence of a catalyst in the oxidation reactor under conditions sufficient to selectively oxidize sulfur compounds present in the hydrocarbon feedstock to produce a hydrocarbon stream that comprises hydrocarbons and oxidized sulfur-containing compounds;

c. separating the oxidized sulfur-containing hydrocarbon stream into an aqueous phase and a non-aqueous oxidized effluent;

d. recovering the non-aqueous oxidized effluent and contacting it with an electron donor agent to oxidize sulfones and sulfoxides present in the non-aqueous oxidized effluent; and

,

e. separating and recovering the hydrocarbon stream from which the sulfones and sulfoxides have been removed.

2. The process according to claim 1, wherein from about 1 to about 5 mole equivalents of an electron donor agent is used based on the sulfone and sulfoxide content of the feedstock.

3. The process according to claim 2, wherein from about 1 to about 3 mole equivalents of an electron donor agent is used.

4. The process according to claim 1, wherein the decomposition is effected at a temperature from about 100°

C. to about 300°

C.

5. The process according to claim 4, wherein the decomposition is effected at about 100°

C. to about 200°

C.

6. The process according to claim 5, wherein the decomposition is effected about 100°

C. to about 150°

C.

7. The process according to claim 1, wherein the decomposition is conducted at a pressure of about 3 kg/cm² to about 30 kg/cm².

8. The process according to claim 1, wherein the decomposition is conducted at about 0.05 h⁻

1 to about 4.0 h<sup>−

1</sup>.

9. The process according to claim 1, wherein the electron donor agent must have an oxidation potential sufficient to effect reductive cleavage of the sulfones and the sulfoxides.

10. The process according to claim 9, wherein the electron donor is a tetraazaalkene.

11. The process according to claim 8, wherein the bisimidazole is bisimidazolylidene.

12. The process according to claim 1, wherein the hydrocarbon feedstock is crude oil, oil, shale oil, coal liquids, intermediate refinery products and distilled fractions thereof.

13. The process according to claim 9, wherein the electron donor agent has at least a half potential of −

1.2V in dimethylformanide when referenced to a saturated calomel electrode.

14. The process according to claim 12, wherein the hydrocarbon feeds stock boils in the range of about 36°

C. to about 2000°

C.

15. The process according to claim 1, wherein after step c), the non-aqueous oxidized effluent is subjected to solvent extraction.

16. The process according to claim 15, wherein the solvent is a polar solvent.

17. The process according to claim 15, wherein the extraction is conducted between about 20°

C. and about 60°

C. and at a pressure between about 1 and about 10 bars.

18. The process according to claim 15, wherein after the step of extraction, the extracted effluent is subjected to adsorption.

19. The process of claim 18, wherein the adsorbent materials are selected from the group consisting of activated carbon, silica gel, alumina, natural clays, polar polymers applied silica gel, activated carbon and alumina.

20. The process according to claim 18, wherein the adsorption zone is operated between about 20°

C. and about 60°

C. and at a pressure between about 1 and about 15 bars.