Claims
- 1. A process for producing a lubricating oil basestock which comprises:
(a) conducting a lubricating oil feedstock to a solvent extraction zone and under-extracting the feedstock to form an under-extracted raffinate wherein the extraction zone solvent contains water added in the amount from about 1 to about 10 vol. %, based on extraction solvent, such that the extraction solvent contains from 3 to 10 vol. % water; (b) stripping the under-extracted raffinate of solvent to produce an under-extracted raffinate feed having a dewaxed oil viscosity index from about 75 to about 105; (c) passing at least a portion of the raffinate feed to a first hydroconversion zone and processing the raffinate feed in the presence of a non-acidic catalyst at a temperature of from 320 to 420° C., a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), space velocity of 0.2 to 5.0 LHSV and a hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a first hydroconverted raffinate; (d) passing the hydroconverted raffinate from the first hydroconversion zone to a second hydroconversion zone and processing the hydroconverted raffinate in the presence of a non-acidic catalyst at a temperature of from 320 to 420° C. provided that the temperature in the second hydroconversion is not greater than the temperature in the first hydroconversion zone, a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), a space velocity of from 0.2 to 5.0 LHSV and a hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a second hydroconverted raffinate; (e) passing at least a portion of the second hydroconverted raffinate to a hydrofinishing reaction zone and conducting cold hydrofinishing of the second hydroconverted raffinate in the presence of a hydrofinishing catalyst which is at least one Group VIB or Group VIII metal on a refractory metal oxide support at a temperature of from 200 to 360° C., a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), a space velocity of from 0.2 to 10 LHSV and hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a hydrofinished raffinate.
- 2. The process of claim 1 wherein the solvent extraction zone includes an extraction solvent selected from at least one of N-methyl-2-pyrrolidone, furfural and phenol.
- 3. The process of claim 2 wherein the extraction zone conditions include a solvent, oil ratio is from 0.5 to 5.0.
- 4. The process of claim 1 wherein the raffinate feed has a dewaxed oil viscosity index from about 80 to about 95.
- 5. The process of claim 1 wherein the non-acidic catalyst has an acidity less than about 0.5, said acidity being determined by the ability of the catalyst to convert 2-methyl-2-pentene to 3-methyl-2-pentene and 4-methyl-2-pentene and is expressed as the mole ratio of 3-methyl-2-pentene to 4-methyl-2-pentene.
- 6. The process of claim 1 wherein the non-acidic catalyst in the first hydroconversion zone is at least one of a Group VIB metal and non-noble Group VIII metal.
- 7. The process of claim 1 wherein the space velocity in the first and second hydroconversion zones is from about 0.3 to 3.0 LHSV.
- 8. The process of claim 1 wherein the temperature in the second hydroconversion zone is about 5 to 100° C. lower than the temperature in the first hydroconversion zone.
- 9. The process of claim 1 wherein the temperature in the hydrofinishing zone is from about 290 to 350° C.
- 10. The process of claim 1 wherein the catalyst in the hydrofinishing zone includes at least one Group VIII noble metal.
- 11. The process of claim 10 wherein the catalyst is Pt, Pd or a mixture thereof.
- 12. The process of claim 1 wherein the second hydroconverted raffinate is passed to a separator to separate low boiling products from hydroconverted raffinate prior to passing to the hydrofinishing reaction zone.
- 13. The process of claim 12 wherein hydroconverted raffinate from the separator is passed to a dewaxing zone and subjected to at least one of solvent dewaxing and catalytic dewaxing prior to passing to the hydrofinishing zone.
- 14. The process of claim 13 wherein catalytic dewaxing is accomplished with a dewaxing catalyst containing at least one 10 ring molecular sieve.
- 15. The process of claim 1 wherein the second hydroconverted raffinate is passed to a dewaxing zone and catalytically dewaxed using a sulfur and nitrogen tolerant molecular sieve prior to passing to the hydrofinishing zone.
- 16. The process of claim 1 wherein the hydrofinished raffinate is passed to a separator to separate low boiling products from the hydrofinished raffinate to produce a second hydrofinished raffinate.
- 17. The process of claim 16 wherein the second hydrofinished raffinate is passed to a dewaxing zone and subjected to at least one of solvent dewaxing and catalytic dewaxing to produce a dewaxed second hydrofinished raffinate.
- 18. The process of claim 17 wherein the catalytic dewaxing is accomplished with a dewaxing catalyst containing at least one 10 ring molecular sieve.
- 19. The process of claim 1 wherein the hydrofinished raffinate is passed to a dewaxing zone and dewaxed using a sulfur and nitrogen tolerant molecular sieve.
- 20. The process of claim 17 wherein the dewaxed second hydrofinished raffinate is further hydrofinished in a second hydrofinishing zone.
- 21. The process of claim 1 wherein the under-extracted raffinate feed is solvent dewaxed under solvent dewaxing conditions prior to entering the first hydroconversion zone.
- 22. The process of claim 1 additionally comprising adding additives to the lubricating oil basestock.
- 23. The process of claim 22 wherein the additives comprise at least one detergent, dispersant, antioxidant, friction modifier, demulsifier, VI improver and antifoamant.
- 24. The process of claim 1 wherein second hydroconversion zone additionally contains a catalytic dewaxing catalyst.
- 25. A process for producing a lubricating oil basestock which comprises:
(a) conducting a lubricating oil feedstock, said feedstock being a distillate fraction, to a solvent extraction zone and under-extracting the feedstock to form an under-extracted raffinate; (b) stripping the under-extracted raffinate of solvent to produce an under-extracted raffinate feed having a dewaxed oil viscosity index from about 75 to about 105; (c) passing at least a portion of the raffinate feed to a hydroconversion zone and hydroconverting the raffinate feed under hydroconversion conditions to produce a basestock containing at least about 90% saturates and a VI less than about 120, said basestock having volatility-viscosity properties characterized by the equation N=(32−(4)(V))±1 where N is the Noack volatility and V is the viscosity in the range 3.5 to 6.0 cSt at 100° C.
- 26. A process for producing a lubricating oil basestock which comprises:
(a) conducting a lubricating oil feedstock to a solvent extraction zone and under-extracting the feedstock to form an under-extracted raffinate wherein the extraction zone solvent contains water added in the amount from about 1 to about 10 vol. %, based on extraction solvent, such that the extraction solvent contains from 3 to 10 vol. % water; (b) stripping the under-extracted raffinate of solvent to produce an under-extracted raffinate feed having a dewaxed oil viscosity index from about 75 to about 105; (c) passing at least a portion of the raffinate feed to a first hydroconversion zone and processing the raffinate feed in the presence of a non-acidic catalyst at a temperature of from 320 to 420° C., a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), space velocity of 0.2 to 5.0 LHSV and a hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a first hydroconverted raffinate; (d) passing the hydroconverted raffinate from the first hydroconversion zone to a second hydroconversion zone and processing the hydroconverted raffinate in the presence of a non-acidic catalyst at a temperature of from 320 to 420° C. provided that the temperature in the second hydroconversion is not greater than the temperature in the first hydroconversion zone, a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), a space velocity of from 0.2 to 5.0 LHSV and a hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a second hydroconverted raffinate; (e) passing at least a portion of the second hydroconverted raffinate to a dewaxing zone and conducting at least one of catalytic and solvent dewaxing under dewaxing conditions to produce a dewaxed hydroconverted raffinate; (f) passing at least a portion of the dewaxed hydroconverted raffinate to a hydrofinishing reaction zone and conducting cold hydrofinishing of the second hydroconverted raffinate in the presence of a hydrofinishing catalyst which is at least one Group VIB or Group VIII metal on a refractory metal oxide support at a temperature of from 200 to 360° C., a hydrogen partial pressure of from 1000 to 2500 psig (7.0 to 17.3 mPa), a space velocity of from 0.2 to 10 LHSV and hydrogen to feed ratio of from 500 to 5000 Scf/B (89 to 890 m3/m3) to produce a hydrofinished raffinate.
Priority Claims (1)
Number |
Date |
Country |
Kind |
US00/13433 |
May 2000 |
US |
|
CROSS-REFERENCE TO RELATED APPLICATION
[0001] This is a continuation-in-part of U.S. Ser. No. 09/532,377 filed Mar. 21, 2000 which is a continuation-in-part of U.S. Ser. No. 09/318,075 filed May 25, 1999 which is a divisional of U.S. patent application Ser. No. 08/768,252, filed Dec. 17, 1996, and this application claims priority to International Patent Application No. US00/13433, filed May 16, 2000.
Divisions (1)
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Number |
Date |
Country |
Parent |
08768252 |
Dec 1996 |
US |
Child |
09318075 |
May 1999 |
US |
Continuation in Parts (2)
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Number |
Date |
Country |
Parent |
09532377 |
Mar 2000 |
US |
Child |
09737044 |
Dec 2000 |
US |
Parent |
09318075 |
May 1999 |
US |
Child |
09532377 |
Mar 2000 |
US |