Method for manufacturing cleaner fuels

• US 6,248,230 B1
• Filed: 06/24/1999
• Issued: 06/19/2001
• Est. Priority Date: 06/25/1998
• Status: Expired due to Term

• Current Assignee: SK Energy Corporation (SK Innovation Company Limited)
• Original Assignee: SK Corporation (Kimberly-Clark Corporation)
• Inventors: Ryu, Jae-Wook, Yoo, Kwan-Sik, Min, Dong-Soon, Min, Wha-Sik, Choi, Kyung-Il, Khang, Sin-Young, Kim, Jyu-Hwan
• Primary Examiner(s): Yildirim, Bekir L.
• Application Number:
  US09/339,639
• Time in Patent Office: 726 Days
• Field of Search: 208/87, 208/91, 208/108, 208/211, 208/213, 208/254.R
• US Class Current: 208/213
• CPC Class Codes: C10G 67/04 including solvent extraction as the refining step in the absence of hydrogen
• CPC Class Codes: C10G 67/06 including a sorption process as the refining step in the absence of hydrogen

Abstract

A method is provided for manufacturing cleaner fuels, in which NPC (Natural Polar Compounds), naturally existing in small quantities within various petrolic hydrocarbon fractions, are removed from the petrolic hydrocarbon fractions ranging, in boiling point, from 110 to 560° C. and preferably from 200 to 400° C., in advance of catalytic hydroprocessing. The removal of NPC improves the efficiency of the catalytic process and produces environment-friendly products, such as diesel fuel with a sulfur content of 50 ppm (wt) or lower. Also, the NPC can be used to improve fuel lubricity.

Claims

1. A method of manufacturing hydrocarbon fuel, the method comprising:

(a) removing natural polar compounds from a petroleum feedstock fraction prior to catalytically hydroprocessing the petroleum feedstock fraction to substantially decrease the concentration of natural polar compounds in the petroleum feedstock fraction, the petroleum feedstock fraction having a boiling point in the range from 110°

C. to 560°

C., and (b) catalytically hydroprocessing the petroleum feedstock fraction to produce a hydrocarbon fuel.

2. The method of claim 1, wherein the hydrocarbon fuel has a boiling point in the range of 110°

C. to 400°

C. and a sulfur content less than 500 ppm (wt).

3. The method of claim 1, wherein the hydrocarbon fuel has a boiling point in the range of 110°

C. to 400°

C. and a sulfur content less than 50 ppm (wt).

4. The method of claim 1, wherein the boiling point of the petroleum feedstock fraction is in the range from 200°

C. to 400°

C.

5. The method of claim 1, wherein the petroleum feedstock fraction resulting from step (a) contains greater than a 30% reduction in nitrogen content, greater than a 0.5% reduction in sulfur content, and greater than a 60% reduction in total acid number, as compared to the original feedstock fraction.

6. The method of claim 1, wherein the natural polar compounds comprise between 5.0 and 50% (wt) oxygen-containing compounds, between 5.0 and 50% (wt) nitrogen-containing heterocyclic compounds, and sulfur content in the range of 0.1 to 5.0% (wt).

7. The method of claim 1, wherein the natural polar compounds removed from the petroleum feedstock fraction constitute between 0.1 to 5.0% (wt) of the petroleum feedstock fraction.

8. The method of claim 1, wherein hydroprocessing is selected from the group of processes consisting of hydrodesulfurizing, hydrodearomatizing, mild hydrocracking, hydrocracking, or mixtures thereof.

9. The method of claim 1, wherein the natural polar compounds are removed from the petroleum feedstock fraction by solvent extraction.

10. The method of claim 9, wherein the petroleum feedstock contains heavy gas oils having a final boiling point over 400°

C., fluidized catalytic cracking (FCC) cycle oil, and coker gas oil.

11. The method of claim 1, wherein the natural polar compounds are removed from the petroleum feedstock fraction by adsorption with one or more adsorbents.

12. The method of claim 11, wherein the adsorption occurs in two or more adsorption towers.

13. The method of claim 11, wherein the adsorption process occurs in a fluidized bed adsorption process or an ebullated bed adsorption process.

14. The method of claim 11, wherein the adsorbent is selected from the group consisting of activated alumina, acid white clay, Fuller'"'"'s earth, activated carbon, zeolite, hydrated alumina, silica gel, ion exchange resin, and combinations thereof.

15. The method of claim 14, wherein the adsorbent is selected from the group consisting of silica gel, ion exchange resin, and combinations thereof.

16. The method of claim 15, wherein the adsorbent is silica gel, having a pore size ranging from 40 to 200 Å

, a specific surface area ranging from 100 to 1000 m²/g, and a pore volume ranging from 0.5 to 1.5 cc/g.

17. A method for improving the lubricity of diesel fuels, the method comprising adding natural polar compounds extracted from petrolic hydrocarbons having a boiling point in the range of 200°

C. to 400°

C.

18. The method as set forth in claim 17, wherein the natural polar compounds are concentrated by adsorption.

19. The method of claim 18 where adsorption is selected from the group of processes consisting of fixed bed adsorption using two or more adsorption towers, fluidizing bed adsorption, or an ebullated bed adsorption process.

20. The method of claim 19, wherein the adsorption process utilizes an adsorbent selected from the group consisting of activated alumina, acid white clay, Fuller'"'"'s Earth, activated carbon, zeolite, hydrated alumina, silica gel, ion exchange resin and the combinations thereof.

21. The method of claim 20 wherein the adsorbent is silica gel which having a pore size ranging from 40 to 200 Å

, a specific surface area ranging from 100 to 1,000 m²/g, and a pore volume ranging from 0.5 to 1.5 cc/g.

22. The method as set forth in claim 18, wherein the natural polar compounds have a nitrogen content 50 times greater than that of the petrolic hydrocarbons and comprise greater than 10 wt % oxygen-containing organic acids and phenols.