Claims
- 1. A process of upgrading a cracked, olefinic sulfur-containing feed fraction boiling in the gasoline boiling range while co-processing a light cycle oil, which method comprises:
- contacting a hydrocarbon feed comprising (i) a naphtha component boiling in the gasoline boiling range, which is a cracked, olefinic sulfur-containing feed fraction and (ii) a minor amount of a light cycle oil component having a boiling range within the range of 550.degree. to 800.degree. F., with a hydrodesulfurization catalyst in a first reaction zone, operating under a combination of elevated temperature, elevated pressure and an atmosphere comprising hydrogen, to produce an intermediate product comprising a normally liquid fraction which has a reduced sulfur content and a reduced octane number as compared to the feed;
- contacting the intermediate product in a second reaction zone with an acidic catalyst comprising zeolite beta, to convert at least a part of the intermediate product to a product comprising a fraction boiling in the gasoline boiling range having a higher octane number than the gasoline boiling range fraction of the intermediate product.
- 2. The process as claimed in claim 1 in which the naphtha component of the feed comprises a full range catalytically cracked naphtha fraction having a boiling range within the range of C.sub.5 to 420.degree. F.
- 3. The process as claimed in claim 1 in which the naphtha component of the feed comprises a heavy catalytically cracked naphtha fraction having a boiling range within the range of 330.degree. to 500.degree. F.
- 4. The process as claimed in claim 1 in which the naphtha component of the feed comprises a heavy catalytically cracked naphtha fraction having a boiling range within the range of 330.degree. to 412.degree. F.
- 5. The process as claimed in claim 1 in which the feed fraction comprises a naphtha fraction having a 95 percent point of at least about 380.degree. F.
- 6. The process as claimed in claim 5 in which the feed fraction comprises a naphtha fraction having a 95 percent point of at least about 400.degree. F.
- 7. The process as claimed in claim 1 in which the zeolite beta is in the aluminosilicate form.
- 8. The process as claimed in claim 1 in which the zeolite beta catalyst includes metal hydrogenation component.
- 9. The process as claimed in claim 8 in which the metal component comprises molybdenum or tungsten.
- 10. The process as claimed in claim 9 in which the Group VI metal is molybdenum which is present in an amount from about 2 to 10 weight percent of the catalyst.
- 11. The process as claimed in claim 1 in which the feed comprises the naphtha component and up to 20 volume percent of the light cycle oil component.
- 12. The process as claimed in claim 1 in which the hydrodesulfurization is carried out at a temperature of about 400.degree. to 800.degree. F., a pressure of about 50 to 1500 psig, a space velocity of about 0.5 to 10 LHSV, and a hydrogen to hydrocarbon ratio of about 500 to 5000 standard cubic feet of hydrogen per barrel of feed.
- 13. The process as claimed in claim 1 in which the second stage upgrading is carried out at a temperature of about 300.degree. to 900.degree. F., a pressure of about 50 to 1500 psig, a space velocity of about 0.5 to 10 LHSV, and a hydrogen to hydrocarbon ratio of about 0 to 5000 standard cubic feet of hydrogen per barrel of feed.
- 14. The process as claimed in claim 13 in which the second stage upgrading is carried out at a temperature of about 350.degree. to 850.degree. F., a pressure of about 300 to 1000 psig, a space velocity of about 1 to 6 LHSV, and a hydrogen to hydrocarbon ratio of about 100 to 3000 standard cubic feet of hydrogen per barrel of feed.
- 15. A process for simultaneously upgrading (i) a catalytically cracked, olefinic sulfur-containing feed fraction boiling in the gasoline boiling range and (ii) a light cycle oil fraction having a boiling range in the range of 500.degree. to 850.degree. F., which process comprises:
- hydrodesulfurizing a hydrocarbon feed of:
- (i) a naphtha component boiling in the gasoline boiling range and comprising a cracked, olefinic, sulfur-containing gasoline feed having a sulfur content of at least 50 ppmw, an olefin content of at least 5 percent and a 95 percent point of at least 325.degree. F., and
- (ii) a cycle oil component comprising from 1 to 20 volume percent, based on the volume of the feed, of a light cycle oil fraction produced by the catalytic cracking of a hydrocarbon feed, the light cycle oil fraction having a boiling range in the range of 500.degree. to 850.degree. F. and an API gravity from 8 to 30 and a hydrogen content from 6 to 12 percent, the hydrodesulfurization being carried out with a hydrodesulfurization catalyst in a hydrodesulfurization zone, operating under a combination of elevated temperature, elevated pressure and an atmosphere comprising hydrogen, to produce an intermediate product comprising a normally liquid fraction which has a reduced sulfur content and a reduced octane number as compared to the feed;
- contacting the intermediate product in a second reaction zone with a bifunctional catalyst having acidic and hydrogenation functionality, comprising zeolite beta and a metal hydrogenation component, to convert the intermediate product to a product comprising a fraction boiling in the gasoline boiling range having a higher octane number than the gasoline boiling range fraction of the intermediate product.
- 16. The process as claimed in claim 15 in which the naphtha component has a 95 percent point of at least 350.degree. F., an olefin content of 10 to 20 weight percent, a sulfur content from 100 to 25,000 ppmw and a nitrogen content of 5 to 250 ppmw.
- 17. The process as claimed in claim 15 in which the hydrodesulfurization is carried out at a temperature of about 500.degree. to 800.degree. F., a pressure of about 300 to 1000 psig, a space velocity of about 1 to 6 LHSV, and a hydrogen to hydrocarbon ratio of about 1000 to 2500 standard cubic feet of hydrogen per barrel of feed and the second stage upgrading is carried out at a temperature of about 350.degree. to 900.degree. F., a pressure of about 300 to 1000 psig, a space velocity of about 1 to 6 LHSV, and a hydrogen to hydrocarbon ratio of about 100 to 3000 standard cubic feet of hydrogen per barrel of feed.
- 18. The process as claimed in claim 15 in which the bifunctional catalyst includes a base metal of Group VI of the Periodic Table as the hydrogenation component.
- 19. The process as claimed in claim 15 in which the hydrogenation component is molybdenum.
- 20. The process as claimed in claim 19 in which the hydrogenation component is molybdenum which is present in an amount of from 2 to 10 weight percent of the catalyst.
CROSS REFERENCE TO RELATED APPLICATIONS
This application is a continuation-in-part of prior application Ser. No. 07/891,124, filed Jun. 1, 1992 pending which, in turn, is a continuation-in-part of prior application Ser. No. 07/850,106, filed Mar. 12, 1992, pending, which, in turn, is a continuation-in-part of prior application Ser. No. 07/745,311, filed Aug. 15, 1991, now U.S. Pat No. 0,346,609 issued Sep. 13, 1994. This application is also a continuation-in-part of Ser. Nos. 07/850,106 and 07/745,311, now U.S. Pat. No. 5,346,609. This application is also related to co-pending application Ser. No. 08/133,403, filed Oct. 8, 1993.
US Referenced Citations (13)
Continuation in Parts (3)
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Number |
Date |
Country |
Parent |
891124 |
Jun 1992 |
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Parent |
850106 |
Mar 1992 |
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Parent |
745311 |
Aug 1991 |
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