Demetalation, desulfurization, and decarbonization of petroleum oils by hydrotreatment in a dual bed system prior to cracking

• US 4,447,314 A
• Filed: 05/05/1982
• Issued: 05/08/1984
• Est. Priority Date: 05/05/1982
• Status: Expired due to Fees

• Current Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Original Assignee: Mobil Oil Corporation (Exxon Mobil Corporation)
• Inventors: Banta, Frederick
• Primary Examiner(s): Gantz, Delbert E.
• Assistant Examiner(s): Chaudhuri, O.
• Application Number:
  US06/375,079
• Time in Patent Office: 734 Days
• Field of Search: 208/89, 208/216 PP, 208/251 H
• US Class Current: 208/89
• CPC Class Codes: B01J 35/60 characterised by their surface properties or porosity
• CPC Class Codes: B01J 35/615 100-500 m2/g
• CPC Class Codes: B01J 35/635 0.5-1.0 ml/g
• CPC Class Codes: B01J 35/647 2-50 nm
• CPC Class Codes: C10G 2300/107 Atmospheric residues having a boiling point of at least about 538 °C

Abstract

A process is described for hydrotreating residual oil fractions in an improved dual bed catalyst system comprising a first large-pore catalyst and a second small-pore catalyst in which at least the second catalyst and preferably both catalysts have a quadrulobal shape. Using cobalt and molybdenum composited on alumina as these catalysts, residua are demetalized, desulfurized, and reduced in carbon residue, whereby hitherto unusable residue can be hydroprocessed.

Claims

1. In the preparation of suitable feed stocks for catalytic cracking, an improved process for reducing Conradson carbon content, metals content, and sulfur content in residual oils in order to convert said oils into said suitable feed stocks, comprising:

A. passing a mixture of hydrogen and said oils at hydrogen pressure of about 500 to 3000 psig, a temperature of about 600°

to 850°

F., and a space velocity of 0.1 to 5.0 LHSV, through a trickle bed of first catalyst, said first catalyst comprising the oxides or sulfides of a Group VIB metal and an iron group metal on a support comprising a delta or theta phase alumina, said first catalyst having also at least about 60 percent of its pore volume in pores with diameters of about 100 to 200 A, at least about 5 percent of its pore volume in pores greater than 500 A, and a surface area of up to about 110 m² /g; and

B. then passing said mixture of hydrogen and said oils through a bed of second catalyst disposed downstream of said first catalyst, said second catalyst comprising the oxides or sulfides of a Group VIB metal and an iron group metal on an alumina support, said second catalyst having a surface area of at least 150 m² /g, a quadrulobe shape, and at least 50 percent of its pore volume in pores with diameters of 30 to 100 A.

2. A process as claimed in claim 1 wherein said first catalyst occupies 40% to 80% of the total catalyst volume and has a quadrulobe shape.

3. The process as claimed in claim 1 wherein said first catalyst and said second catalyst are contained in one reactor.

4. The process as claimed in claim 1 wherein said first catalyst and said second catalyst are contained in separate reactors.

5. The process as claimed in claim 2 wherein said first catalyst and said second catalyst are contained in one reactor.

6. The process as claimed in claim 2 wherein said first catalyst and said second catalyst are contained in separate reactors.

7. The process of claim 2 wherein said process includes the step of cracking said oil following said demetalation and desulfurization steps, said cracking being done at 800°

to 1500°

F. temperature, 1 to 5 atmospheres pressure and a space velocity of about 1 to 1000 WHSV.

8. The process of claim 2 wherein said process includes the step of hydrocracking said oil following said demetalation and desulfurization steps, said hydrocracking being done at 400°

to 1000°

F. temperature and 100 to 3500 psig pressure.

9. In a process for converting residual oils to suitable catalytic cracking feedstocks by reducing metals content and sulfur content by the following steps:

A. passing a mixture of hydrogen and said oils at a hydrogen pressure of about 500 to 3000 psig, a temperature of about 600°

to 850°

F., and a space velocity of 0.1 to 5.0 LHSV through a trickle bed of first catalyst, said first catalyst comprising the oxides or sulfides of a group VIB metal and an iron group metal on a support comprising a delta or theta phase alumina, said first catalyst having also at least about 60% of its pore volume in pores with diameters of about 100 to 200 A, at least about 5% of its pore volume in pores greater than 500 A, and a surface area of up to about 110 m² /g; and

B. then passing said mixture of hydrogen and said oils through a bed of second catalyst disposed downstream of said first catalyst, said second catalyst comprising the oxides or sulfides of the Group VIB metal and an iron group metal on an alumina support, said second catalyst having also a surface area of at least 150 m² /g and at least 50% of its pore volume in pores with diameters of 30 to 100 A,

the improvement for additionally reducing the Conradson carbon content of said residual oils, comprising the use of a quadrulobe shape for said second catalyst.

10. The improvement in the process of claim 9, wherein said Conradson carbon reduction is improved by a factor of one third.

11. The improvement in the process of claim 10, wherein said Conradson carbon reduction is effective at temperatures of about 675°

-775°

F.

12. The improvement in the process of claim 9, wherein said quadrulobe shape is additionally used for said first catalyst.