Process to remove olefins from light hydrocarbon stream by mercaptanization followed by merox removal of mercaptans from the separated stream

Patent metadata

Field	Value
Publication number	US-2021032547-A1
Application number	US-201916527711-A
Country	US
Kind code	A1
Filing date	Jul 31, 2019
Priority date	Jul 31, 2019
Publication date	Feb 4, 2021
Grant date	—

Abstract

A light naphtha feedstock containing olefins is introduced with hydrogen sulfide into a mercaptanization zone for conversion of the olefins into a mercaptan stream that is substantially free of olefins, after which the mercaptans are sent with an alkali caustic solution into a mercaptan oxidation treatment unit (MEROX) to produce a spent caustic stream and sweet light naphtha product stream that is substantially free of olefins and of mercaptans. Disulfide oils are produced from the wet air oxidation of the spent caustic, and the disulfide oils can be further processed to provide high purity olefin building blocks.

First claim

1 . A process for treating an olefin-containing light naphtha feedstock, the process comprising:
a. introducing the light naphtha feedstock containing olefins and hydrogen sulfide into a mercaptanization zone containing a catalyst for reaction of the H 2 S with the olefins to produce a treated effluent stream containing mercaptans that is substantially free of olefins; b. passing the treated effluent stream containing mercaptans and an alkali caustic solution to a mercaptan oxidation treatment zone to produce a spent caustic and alkali metal alkane thiolate mixture stream and a sweet light naphtha product stream that is substantially free of olefins and of mercaptans; c. recovering the sweet light naphtha product stream; d. passing the spent caustic and alkali metal alkane thiolate mixture stream, catalyst, and air into a wet air oxidation zone to product a regenerated spent caustic stream and a disulfide oils product stream; and e. recovering the disulfide oils product stream.

2 . The process of claim 1 , further comprising passing the treated effluent stream to a fractionation zone to produce a light naphtha product stream that is recovered, and a mercaptan stream that is the feed to the mercaptan oxidation unit treatment.

3 . The process of claim 2 , wherein the sweet light naphtha product stream comprises paraffins, naphthenes and aromatics.

4 . The process of claim 2 , wherein the mercaptan stream is substantially free of olefins.

5 . A process for treating an olefin-containing light naphtha feedstock, the process comprising:
a. introducing the light naphtha feedstock containing olefins, an internally-produced mercaptan stream and an alkali caustic solution into a mercaptan oxidation treatment zone to produce a spent caustic and alkali metal alkane thiolate mixture stream and sweet light naphtha product stream that is substantially mercaptan free and comprises olefins; b. passing the spent caustic and alkali metal alkane thiolate mixture stream, catalyst, and air into a wet air oxidation zone to produce a regenerated spent caustic stream and a disulfide oils product stream; c. recovering the disulfide oils product stream; d. passing the sweet light naphtha product stream and hydrogen sulfide into a mercaptanization zone containing a catalyst and catalytically reacting hydrogen sulfide with the olefins to produce a treated effluent stream that is substantially free of olefins; e. passing the treated effluent stream to a fractionation zone and recovering a sweet light naphtha product stream and the internally-produced mercaptan stream of step (a).

6 . The process as in claim 1 , wherein a portion of the regenerated spent caustic stream is recycled and mixed to constitute the alkali caustic solution for introduction into the mercaptan oxidation treatment unit.

7 . The process as in claim 1 , wherein the olefin-containing light naphtha feedstock is selected from the group consisting of light naphtha hydrocarbon streams derived from catalytic reforming, steam cracking, fluid catalytic cracking (FCC), delayed coking or flexi-coking, isomerization, visbreaking, transalkylation, and combinations thereof.

8 . The process as in claim 1 , wherein the olefin-containing light naphtha feedstock has a boiling point in the range of from −10° C. to 80° C.

9 . The process as in claim 1 , wherein the olefin-containing light naphtha feedstock comprises C 5 -C 6 olefins.

10 . The process as in claim 1 , wherein the mercaptanization zone contains a catalyst that is an active phase metal catalyst selected from Periodic Table Groups 4-11 supported by an alumina, silica, silica-alumina, titania, or zeolite support.

11 . The process as in claim 1 , wherein the mercaptanization zone operates at a temperature in the range of from 80° C. to 300° C., at a pressure in the range of from 10 bars to 50 bars, at a liquid hourly space volume (LHSV) in the range of from 1 h −1 to 100 h −1 , and at hydrogen sulfide-to-olefin molar ratios in the range of from 1:1 to 100:1.

12 . The process of claim 3 , wherein the mercaptan stream is substantially free of olefins.

13 . The process as in claim 5 , wherein a portion of the regenerated spent caustic stream is recycled and mixed to constitute the alkali caustic solution for introduction into the mercaptan oxidation treatment unit.

14 . The process as in claim 5 , wherein the olefin-containing light naphtha feedstock is selected from the group consisting of light naphtha hydrocarbon streams derived from catalytic reforming, steam cracking, fluid catalytic cracking (FCC), delayed coking or flexi-coking, isomerization, visbreaking, transalkylation, and combinations thereof.

15 . The process as in claim 5 , wherein the olefin-containing light naphtha feedstock has a boiling point in the range of from −10° C. to 80° C.

16 . The process as in claim 5 , wherein the olefin-containing light naphtha feedstock comprises C 5 -C 6 olefins.

17 . The process as in claim 5 , wherein the mercaptanization zone contains a catalyst that is an active phase metal catalyst selected from Periodic Table Groups 4-11 supported by an alumina, silica, silica-alumina, titania, or zeolite support.

18 . The process as in claim 5 , wherein the mercaptanization zone operates at a temperature in the range of from 80° C. to 300° C., at a pressure in the range of from 10 bars to 50 bars, at a liquid hourly space volume (LHSV) in the range of from 1 h −1 to 100 h −1 , and at hydrogen sulfide-to-olefin molar ratios in the range of from 1:1 to 100:1.

Assignees

• Saudi Arabian Oil Co

Inventors

• Koseoglu Omer Refa

Classifications

• C10G53/12

  including at least one alkaline treatment step · CPC title

• C10G19/02

  with aqueous alkaline solutions · CPC title

• C10G57/00

  Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process · CPC title

• C10G53/10

  including at least one acid-treatment step · CPC title

• C10G29/28

  containing sulfur as the only hetero atom, e.g. mercaptans, or sulfur and oxygen as the only hetero atoms · CPC title