Claims
- 1. A hydrotreating process comprising the steps of:
- hydrotreating a resid feedstock at a temperature between about 700.degree. and 850.degree. F., at a total pressure of between about 2650 and 3050 psig, and at a hydrogen partial pressure of between 1800 and 2300 psig;
- thereafter the hydrotreating step fractionating the hydrotreated feedstock into a hydrotreated resid bottoms fraction and at least one relatively lower boiling fraction;
- thereafter the fractionating step deasphalting the bottoms fraction to remove an asphaltene fraction therefrom; and
- thereafter the deasphalting step deep-vacuum reducing the hydrotreated resid bottoms fraction to produce an oil fraction having an upper boiling point cut-off temperature of at least 1050.degree. F.
- 2. The process of claim 1 wherein the deasphalting step includes solvent extracting the hydrotreated resid bottoms fraction with one or more non-aromatic deasphalting solvents containing three to seven carbon atoms to produce a resin- and oil-rich solvent fraction and the asphaltene fraction.
- 3. The process of claim 2 wherein the deasphalting is accomplished at a temperature above about 50.degree. F. below a critical temperature of the solvent.
- 4. A process for fractionating a bottoms fraction from a resid hydrotreating unit, said bottoms fraction having been hydrotreated in the hydrotreating unit at a temperature between about 700.degree. and 805.degree. F., at a total pressure of between about 2650 and 3050 psig, and at a hydrogen partial pressure of between 1800 and 2300 psig, said process comprising the steps of:
- thereafter the hydrotreating step removing a substantial portion of material boiling below 850 degrees Fahrenheit from the hydrotreated resid bottoms fraction;
- thereafter deasphalting the bottoms fraction to produce an asphaltene fraction and a resin- and oil-rich fraction; and
- thereafter the deasphalting step deep-vacuum reducing the resin- and oil-rich fraction to produce an oil overhead fraction having an upper boiling point cut-off temperature of at least 1050.degree. F. and a resin bottoms fraction.
- 5. The process of claim 4 wherein the deasphalting step includes solvent extracting the bottoms fraction with one or more alkane solvents containing three to seven carbon atoms at a temperature above about 50.degree. F. degrees below the critical temperature of the solvent.
- 6. The process of claim 5 wherein the solvent contains four or five carbon atoms.
- 7. The process of claim 4 wherein the hydrotreated resid bottoms fraction is produced by reacting a virgin resid in an ebullated bed reactor in the presence of a hydrocracking catalyst and a hydrogen-rich gas and thereafter removing the substantial portion of material boiling below 850 degree Fahrenheit by distillation.
- 8. The process of claim 4 wherein the deasphalting step includes the steps of:
- solvent extracting the bottoms fraction with an alkane solvent containing three to seven carbon atoms at a temperature above about 50 degrees below the critical temperature of the solvent to produce the asphaltene fraction and the resin- and oil-rich solvent fraction;
- separating the asphaltene fraction from the resin- and oil-rich solvent fraction; and
- increasing the temperature of the resin- and oil-rich solvent fraction to at least 50 degrees above the critical temperature of the solvent to produce a solvent fraction and a resin and oil fraction.
- 9. The process of claim 8 wherein the solvent is n-pentane.
- 10. The process of claim 4 wherein the substantial portion of 850 degree Fahrenheit minus products are separated from the hydrotreated resid by atmospheric and vacuum distillation.
- 11. The process of claim 4 wherein a substantial portion of the oil fraction produced by deep vacuum reduction boils below about 1150 degrees Fahrenheit at atmospheric pressure.
- 12. A process for hydrotreating a resid and producing an oil feedstock therefrom comprising the steps of:
- hydrotreating a virgin resid feedstream by reacting the resid in an ebullated bed reactor in the presence of a hydrocracking catalyst and a hydrogen-rich gas at a temperature between about 700.degree. and 850.degree. F., at a total pressure of between about 2650 and 3050 psig, and at a hydrogen partial pressure of between 1800 and 2300 psig to produce a hydrotreated effluent stream;
- thereafter the hydrotreating step removing a substantial portion of material boiling below 1000 degrees Fahrenheit from the hydrotreated effluent stream by distillation, thereby producing a hydrotreated resid bottoms fraction;
- thereafter the distilling step solvent extracting the bottoms fraction with an alkane solvent containing three to seven carbon atoms at a temperature above about 20 degrees below the critical temperature of the solvent to produce an asphaltene fraction and a resin- and oil-rich solvent fraction;
- thereafter the solvent extracting step separating the asphaltene fraction from the resin- and oil-rich solvent fraction; and
- increasing the temperature of the resin- and oil-rich solvent fraction to at least 50 degrees above the critical temperature of the solvent to produce a solvent fraction and a resin and oil fraction; and
- thereafter the separating step deep-vacuum reducing the resin- and oil-rich fraction to produce a resin bottoms fraction and an overhead oil fraction containing a substantial portion of material having an upper boiling point cut-off temperature below about 1200 degrees Fahrenheit at atmospheric pressure.
- 13. The process of claim 12 wherein the solvent is n-pentane.
- 14. The process of claim 12 wherein the virgin resid feedstream is a bottoms fraction from the vacuum reduction of crude oil.
- 15. The process of claim 12 wherein a distillation in the removing step is a vacuum distillation.
- 16. The process of claim 12 wherein a substantial portion of the oil fraction produced by deep vacuum reduction boils below about 1150 degrees Fahrenheit, at atmospheric pressure.
- 17. The process of claim 12 wherein at least a portion of the resin fraction is recycled to the ebullated bed reactor to solvate virgin resid fed into the reactor.
- 18. The process of claim 12 wherein the distilled oil fraction is thereafter processed by catalytically cracking the oil in a fluidized catalytic cracking unit, or first pretreating the oil in a catalytic feed hydrotreating unit and then catalytically cracking effluent from the hydrotreating unit.
Parent Case Info
This application is a continuation-in-part of U.S. application Ser. No. 07/610,936 filed Nov. 9, 1990 now U.S. Pat. No. 5,124,024, and a continuation-in-part of U.S. application Ser. No. 07/616,219 filed Nov. 20, 1990 now U.S. Pat. No. 5,124,025, and a continuation-in-part of U.S. application Ser. No. 07/616,208 filed Nov. 20, 1990, now U.S. Pat. No. 5,124,026, and a continuation-in-part of U.S. application Ser. No. 07/318,372 filed Jul. 18, 1989 now U.S. Pat. No. 5,013,427 and a continuation-in-part of U.S. application Ser. No. 07/824,289 filed Jan. 23, 1992 now U.S. Pat. No. 5,242,578 and a continuation-in-part of U.S. application Ser. No. 07/824,508 filed Jan. 23, 1992, now U.S. Pat. No. 5,228,978 and a continuation-in-part of U.S. application Ser. No. 07/824,509 filed Jan. 23, 1992 now U.S. Pat. No. 5,258,117, and a continuation-in-part of U.S. application Ser. No. 07/618,218 filed Nov. 20, 1990 now U.S. Pat. No. 5,124,027.
US Referenced Citations (8)
Continuation in Parts (1)
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Number |
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610936 |
Nov 1990 |
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