Process scheme for the production of optimal quality distillate for olefin production

Patent metadata

Field	Value
Publication number	US-10711208-B2
Application number	US-201715628086-A
Country	US
Kind code	B2
Filing date	Jun 20, 2017
Priority date	Jun 20, 2017
Publication date	Jul 14, 2020
Grant date	Jul 14, 2020

Abstract

Systems and processes for hydrotreating, splitting, and extracting a gasoil feed to produce a saturate-rich feedstock for olefin pyrolysis are provided. A gasoil feed is provided to a hydrotreating section to produce an ultralow sulfur distillate (ULSD) stream. The ULSD stream is provided to a splitter section to produce a light distillate stream and a heavy bottom stream. The light distillate stream is provided to an extraction section to produce an aromatic-rich extract phase and a saturate-rich raffinate phase. The raffinate phase is mixed with the heavy bottom stream to produce an olefin pyrolysis feedstock having a reduced BMCI as compared to the gasoil feed stream and the ULSD stream.

First claim

What is claimed is:

1. A method of producing a feedstock for olefin pyrolysis, comprising:
hydrotreating a gasoil feed with a hydrotreating catalyst in the presence of hydrogen to produce an ultralow sulfur distillate (ULSD) stream comprising less than 10 parts-per-million weight (ppmw) sulfur, less than 10 ppmw nitrogen, and maximum aromatic saturation as compared to the gasoil feed such that greater than 95% by weight of the aromatics in the ULSD stream are monoaromatics;
separating, via a tray distillation column, the ULSD stream into a light distillate stream and a heavy bottom stream, wherein aromatics in the light distillate stream comprise at least 50% by weight monoaromatics and aromatics in the heavy bottom stream comprise no more than 15% by weight monoaromatics;
extracting, in an extraction section, an extract phase and a raffinate phase from the light distillate stream, the raffinate phase comprising at least 50% by weight saturated hydrocarbons and no more than 15% by weight aromatics, the extraction section comprising a liquid-liquid extraction (LLE) column, secondary re-extract column, an extract and raffinate wash column, a distillation column, and a solvent recovery column; and
mixing the raffinate phase with the heavy bottom stream produced from the separation of the ULSD stream to produce the feedstock for olefin pyrolysis, wherein a Bureau of Mines Correlation Index (BMCI) of the feedstock for olefin pyrolysis is less than the BMCI of the gasoil feed and the BMCI of the ULSD stream.

2. The method of claim 1 , wherein the light distillate stream has a true boiling point (TPB) in the range of 140° C. to about 300° C.

3. The method of claim 1 , wherein the heavy bottom stream has a true boiling point (TPB) in the range of 300° C. to about 400° C.

4. The method of claim 1 , wherein the gasoil feed has a true boiling point (TPB) in the range of about 140° C. to about 400° C.

5. The method of claim 1 , wherein the hydrotreating is performed at a temperature in the range of 200° C. to 450° C. and a pressure in the range of 34 barg to 100 barg.

6. The method of claim 1 , wherein the hydrotreating catalyst is a heterogeneous fixed bed catalyst comprising at least one Group VIII metal and at least one Group VIB metal.

7. The method of claim 6 , wherein the at least one Group VIII metal is selected from the group consisting of iron, cobalt and nickel and the at least one Group VIB metal is selected from the group consisting of molybdenum and tungsten.

8. The method of claim 1 , comprising stripping a reactor effluent from the hydrotreating using a stripping column, wherein the stripping is performed at a temperature in the range of about 40° C. to 400° C. and a pressure in the range of about 0.05 barg to about 20 barg.

9. The method of claim 1 , wherein extracting the extract phase and the raffinate phase via the liquid-liquid extraction (LLE) column comprises using a first solvent and a second solvent.

10. The method of claim 9 , wherein the first solvent comprises N-Methyl-2-pyrrolidone (NMP) or dimethyl sulfoxide (DMSO).

11. The method of claim 9 , wherein the second solvent comprises paraffinic light naphtha or C6 and C7 hydrocarbons.

12. The method of claim 1 , wherein the extract phase comprises at least 50% by weight aromatics.

13. A method of processing hydrocarbons, comprising
providing a gasoil feed to a hydrotreating section with a hydrotreating catalyst to produce an ultralow sulfur distillate (ULSD) stream, the ultralow sulfur distillate stream comprising less than 10 parts-per-million weight (ppmw) sulfur, less than 10 ppmw nitrogen, and maximum aromatic saturation as compared to the gasoil feed such that greater than 95% by weight of the aromatics in the ULSD stream are monoaromatics;
providing the ULSD stream to a splitter section to produce a light distillate stream and a heavy bottom stream, wherein the aromatics in the light distillate stream comprise at least 50% by weight monoaromatics and the aromatics in the heavy bottom stream comprise no more than 15% by weight monoaromatics;
providing the light distillate stream to an extraction section to produce an extract phase and a raffinate phase, the raffinate phase comprising at least 50% by weight saturated hydrocarbons and no more than 15% by weight aromatics, the extraction section comprising a liquid-liquid extraction (LLE) column, secondary re-extract column, an extract and raffinate wash column, a distillation column, and a solvent recovery column; and
obtaining a feed stream for olefin pyrolysis, the feed stream comprising the raffinate phase and the heavy bottom stream produced from the ULSD stream, wherein a Bureau of Mines Correlation Index (BMCI) of the feedstock for olefin pyrolysis is less than the BMCI of the gasoil feed and the BMCI of the ULSD stream.

14. The method of claim 13 , wherein the gasoil feed has a true boiling point (TPB) in the range of about 140° C. to about 400° C.

15. The method of claim 13 , wherein the hydrotreating catalyst is a heterogeneous fixed bed catalyst comprising at least one Group VIII metal and at least one Group VIB metal.

16. The method of claim 13 , wherein the extract phase comprises at least 50% by weight aromatics.

Assignees

• Saudi Arabian Oil Co

Inventors

• Ramaseshan Vinod
• Beadle Bruce R
• Killingworth Marcus J
• Al-Ghamdi Abdulaziz S

Classifications

• Y02P30/40

  Ethylene production · CPC title

• C10G21/22

  Compounds containing sulfur, selenium, or tellurium · CPC title

• C10G2400/06

  Gasoil · CPC title

• C10G45/44

  Hydrogenation of the aromatic hydrocarbons · CPC title

• C10G67/0436 Primary

  The hydrotreatment being an aromatic saturation · CPC title