Conversion of full range crude oils with low molecular weight carbon-hydrogen fragment contributors over zeolite catalysts

• US 3,974,062 A
• Filed: 10/17/1974
• Issued: 08/10/1976
• Est. Priority Date: 10/17/1974
• Status: Expired due to Term

• Current Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Original Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Inventors: Owen, Hartley, Venuto, Paul B., Rosinski, Edward J.
• Primary Examiner(s): Gantz, Delbert E.
• Assistant Examiner(s): Schmitkons, G. E.
• Application Number:
  US05/515,757
• Time in Patent Office: 663 Days
• Field of Search: 208/120, 208/74, 208/254 R, 208/254 H
• US Class Current: 208/74
• CPC Class Codes: B01J 8/24 according to "fluidised-bed" technique B01J8/20 takes precedence
• CPC Class Codes: C10G 11/18 according to the "fluidised-bed" technique

Abstract

A refinery process is described for converting desalted full range crude oils and syncrudes derived from coal, shale and tar sands. The process involves mixing and reacting the full range heavy oil feed with a low molecular weight carbon-hydrogen fragment contributor such as methanol or C₂ -C₅ olefins in the presence of a fluid zeolite cracking catalyst comprising mordenite.

Claims

1. A method for converting a full boiling range oil charge selected from the group consisting of crude oil and syncrudes derived from coal, shale and tar sands which comprises,

mixing the oil charge with at least 5 weight percent on feed of a low molecular weight carbon-hydrogen fragment contributor selected from the group consisting of methanol alone or in admixture with C₂ -C₅ olefins,

passing the mixture thus formed in contact with a crystalline zeolite cracking catalyst under conversion conditions comprising a temperature within the range of 800°

to 1400°

F. and an oil charge residence time within the range of 0.5 to 12 seconds, and

recovering the products of said cracking operation separate from the catalyst employed therein.

2. The method of claim 1 wherein from about 100 to 200 volume percent of methanol per 100 volume percent of oil charge is employed.

3. The method of claim 1 wherein the crystalline zeolite comprises a faujasite crystalline zeolite.

4. The method of claim 1 wherein the crystalline zeolite comprises a mordenite crystalline zeolite.

5. The method of claim 1 wherein a large pore crystalline zeolite cracking catalyst is employed in combination with a ZSM-5 crystalline zeolite.

6. The method of claim 1 wherein the oil charge comprises a desalted whole crude admixed with from about 5 to about 200 weight percent of C₅ and lighter olefins which is thereafter passed in contact with a mordenite crystalline zeolite cracking catalyst at a temperature within the range of 950°

to about 1050°

F.

7. The method of claim 1 wherein a heavy naphtha product of the cracking operation is recovered and recracked at an elevated temperature in the presence of the carbon-hydrogen fragment contributor to form a higher octane product.

8. The method of claim 1 wherein a heavy cycle oil and a heavy fuel oil product of the cracking operation is recovered and recracked with the full boiling range oil charge to the cracking operation.

9. The method of claim 1 wherein the full boiling range feed boils in the range of -30°

F. to about 1300°

F.

10. The method of claim 7 wherein the cracking of the full boiling range oil charge and the recycled heavy naphtha product of cracking takes place in separate riser reactors relying upon the same catalyst source and product separation zones.

11. The method of claim 1 wherein the crystalline zeolite cracking catalyst comprises a mixture of faujasite and mordenite crystalline zeolites.

12. The method of claim 11 wherein the mordenite crystalline zeolite is used in a major proportion to the faujasite zeolite component.

13. The method of claim 4 wherein the mordenite component is a dealuminized mordenite crystalline zeolite.

14. The method of claim 11 wherein the mordenite component is a dealuminized mordenite crystalline zeolite.