Process for producing needle coke

• US 5,286,371 A
• Filed: 07/14/1992
• Issued: 02/15/1994
• Est. Priority Date: 07/14/1992
• Status: Expired due to Term

• Current Assignee: Amoco Corporation (BP PLC)
• Original Assignee: Amoco Corporation (BP PLC)
• Inventors: Hauschildt, F. W., Venardos, Dean G., Joval, Cheryl L. M., Goval, Shri K., Kolstad, Jeffrey J.
• Primary Examiner(s): Brunsman, David
• Assistant Examiner(s): Yildirim, Bekir L.
• Application Number:
  US07/913,461
• Time in Patent Office: 581 Days
• Field of Search: 208/50, 208/131, 208/51, 208/87, 208/89, 208/56, 208/57, 208/87, 208/131
• US Class Current: 208/131
• CPC Class Codes: C10B 55/00 Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material cracking oils C10G
• CPC Class Codes: C10G 69/00 Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process C10G67/00 takes precedence

Abstract

A process is provided for producing premium and super premium grade needle coke comprising the steps of passing a heavy resid feedstock to a resid hydrotreating reaction zone at resid hydrotreating conditions and producing light resid hydrotreated products and a heavy resid hydrotreated residual product, directing the heavy resid hydrotreated residual product and FCC decanted oil to a solvent extraction process reaction zone at solvent extraction process conditions and producing products comprising a solvent extracted oil and resin stream and a stream comprising asphaltenes, and conveying at least a portion of the solvent extracted oil and resin stream to a delayed coking process at delayed coking conditions and producing liquid products and premium grade coke.

Claims

1. A process for producing needle coke comprising the steps of:

passing a heavy resid feedstock to a resid hydrotreating reaction zone at resid hydrotreating conditions and producing light resid hydrotreated products and a heavy resid hydrotreated residual product;

directing said heavy resid hydrotreated residual product and FCC decanted oil to a solvent extraction process reaction zone at solvent extraction process conditions and producing products comprising a solvent extracted oil and resin stream and a stream comprising asphaltenes; and

conveying at least a portion of said solvent extracted oil and resin stream to a delayed coking process at delayed coking conditions and producing liquid products and needle coke.

2. The process of claim 1 wherein said heavy resid feedstock comprises at least one member selected from the group consisting of high sulfur resid, low sulfur resid, FCC decanted oil, solvent extracted oil and resin, solvent extracted oil, solvent extracted resin, and lubricating oil solvent extraction process extracts.

3. The process of claim 1 wherein said solvent extracted oil and resin stream is further separated into products comprising a solvent extracted oil stream and a solvent extracted resin stream.

4. The process of claim 3 wherein at least a portion of said solvent extracted resin stream is directed to said resid hydrotreating reaction zone.

5. The process of claim 4 wherein said solvent extracted resin stream is directed to said resid hydrotreating reaction zone in a manner so as to maintain said oil and resin stream at a sulfur concentration range of between about 0.01 percent by weight and about 1.0 percent by weight.

6. The process of claim 3 wherein said separation is performed using at least one separation method selected from the group consisting of solvent extraction and distillation.

7. The process of claim 1 wherein at least a portion of said solvent extracted oil and resin stream is directed to a hydrotreating process for hydrotreating under hydrotreating conditions in the presence of a hydrotreating catalyst prior to processing in said delayed coking process.

8. The process of claim 1 wherein said solvent extracted oil and resin stream comprises an aromatics concentration ranging from about 40 percent by weight to about 90 percent by weight, a sulfur concentration ranging from about 0.1 percent by weight to about 1.0 percent by weight, and an ash concentration ranging from about 0.001 percent by weight to about 0.10 percent by weight.

9. The process of claim 1 wherein said FCC decanted oil flow rate to said solvent extraction process reaction zone is controlled in a manner so as to maintain said solvent extracted oil and resin stream at an aromatics concentration range of between about 30 percent by weight and about 85 percent by weight.

10. A process for producing premium grade coke comprising the steps of:

passing a heavy resid feedstock comprising at least one member selected from the group consisting of high sulfur resid, low sulfur resid, FCC decanted oil, solvent extracted oil and resin, solvent extracted oil, solvent extracted resin, and lubricating oil solvent extraction process extracts to a resid hydrotreating reaction zone at resid hydrotreating conditions and producing light resid hydrotreated products and a heavy resid hydrotreated residual product;

directing said heavy resid hydrotreated residual product and FCC decanted oil to a solvent extraction process reaction zone at solvent extraction process conditions and producing products comprising a solvent extracted oil stream, a solvent extracted resin stream, and a stream comprising asphaltenes; and

conveying at least a portion of one or both of said solvent extracted oil stream and said solvent extracted resin stream to delayed coker feedstock for directing to a delayed coking process at delayed coking conditions and producing liquid products and premium grade coke;

wherein said FCC decanted oil is added to at least one or both of said resid hydrotreating reaction zone and said solvent extraction process zone in a manner so as to produce a premium grade coke having a coefficient of thermal expansion of less than about 5×

10^-7 /°

C.

11. The process of claim 10 wherein at least a portion of said solvent extracted resin stream is directed to said resid hydrotreating reaction zone.

12. The process of claim 11 wherein after directing at least a portion of said solvent extracted resin stream to said resid hydrotreating reaction zone, the remaining solvent extracted resin stream along with the solvent extracted oil stream are combined to form a recombined solvent extracted oil and resin stream.

13. The process of claim 12 wherein said FCC decanted oil flow rate to at least one location of said resid hydrotreating reaction zone and said solvent extraction process reaction zone is controlled in a manner so as to maintain said recombined solvent extracted oil and resin stream at an aromatics concentration range of between about 50 percent by weight and about 80 percent by weight.

14. The process of claim 12 wherein said solvent extracted resin stream is directed to said resid hydrotreating reaction zone in a manner so as to maintain said recombined solvent extracted oil and resin stream at a sulfur concentration range of between about 0.01 percent by weight and about 0.7 percent by weight.

15. The process of claim 14 wherein said solvent extracted resin stream is directed to said resid hydrotreating reaction zone in a manner so as to provide for a premium grade coke having dynamic puffing characteristics of less than 2 percent, expressed as the change in deflection of a puffing plug as a percentage of the total length of the plug.

16. The process of claim 13 wherein said FCC decanted oil flow rate to at least one location of said resid hydrotreating reaction zone and said solvent extraction process reaction zone is controlled in a manner so as to provide for a super premium grade coke having a coefficient of thermal expansion of less than about 3×

10^-7 /°

C.

17. The process of claim 10 wherein at least a portion of one or both of said solvent extracted oil stream and said solvent extracted resin stream is directed to a hydrotreating process for hydrotreating at hydrotreating conditions in the presence of a hydrotreating catalyst prior to processing in said delayed coking process.

18. The process of claim 10 wherein said delayed coker feedstock comprises an aromatics concentration ranging from about 50 percent by weight to about 80 percent by weight, a sulfur concentration ranging from about 0.1 percent by weight to about 0.7 percent by weight, and an ash concentration ranging from about 0.001 percent by weight to about 0.10 percent by weight.

19. The process of claim 10 wherein said stream comprising asphaltenes is solvent extracted from said heavy resid hydrotreated residual product and FCC decanted oil, leaving a solvent extracted oil stream and a solvent extracted resin stream, and said solvent extracted oil stream is subsequently separated from said solvent extracted resin stream in a distillation step.

20. The process of claim 10 wherein said solvent extraction process conditions comprise the use of at least one solvent selected from the group consisting of propane and isobutane.