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Hydroconversion process for making lubricating oil basestocks

a technology conversion processes, which is applied in the field of lubricating oil basestocks, can solve the problems of unfavorable toxicity characteristics, low lubricating oil basestocks, and the fact that solvent refining alone produces basestocks with high saturates content, and achieves excellent toxicological properties, low volatility, and good oxidation stability

Inactive Publication Date: 2002-10-24
CODY IAN A +8
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

[0015] The basestocks produced by the process according to the invention have excellent low volatility properties for a given viscosity thereby meeting future industry engine oil standards while achieving good oxidation stability, cold start, fuel economy, and thermal stability properties. In addition, toxicity tests show that the basestock has excellent toxicological properties as measured by tests such as the FDA(c) test.

Problems solved by technology

Thus the crude oils used for solvent refining are restricted to those which are highly paraffinic in nature as aromatics tend to have lower viscosity indices (VI), and are therefore less desirable in lubricating oil basestocks.
Also, certain types of aromatic compounds can result in unfavorable toxicity characteristics.
Today more severe operating conditions for automobile engines have resulted in demands for basestocks with lower volatilities (while retaining low viscosities) and lower pour points.
Nor does solvent refining alone typically produce basestocks with high saturates contents.
In some locations wax isomerization economics can be adversely impacted when the raw stock, slack wax, is highly valued.
Also, the typically low quality feedstocks used in hydrocracking, and the consequent severe conditions required to achieve the desired viscometric and volatility properties can result in the formation of undesirable (toxic) species.

Method used

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  • Hydroconversion process for making lubricating oil basestocks
  • Hydroconversion process for making lubricating oil basestocks
  • Hydroconversion process for making lubricating oil basestocks

Examples

Experimental program
Comparison scheme
Effect test

example 1

[0068] This example illustrates the functions of each reactor A, B and C. Reactors A and B affect VI though A is controlling. Each reactor can contribute to saturates, but Reactor B is primarily used to control saturates. Toxicity and color are controlled in reactor C.

1 TABLE 1 PRIMARY CONTROL Reactor A Reactor B Reactor C VI x Saturates x Toxicity x

example 2

[0069] This example illustrates the product quality of oils obtained from the process according to the invention. Reaction conditions and product quality data for start of run (SOR) and end of run (EOR) are summarized in Tables 2 and 3.

[0070] As can be seen from the data in Table 2 for the 250N feed stock, reactors A and B operate at conditions sufficient to achieve the desired viscosity index, then, with adjustment of the temperature of reactor C, it is possible to keep saturates above 90 wt. % for the entire run length without compromising toxicity (as indicated by DMSO screener result; see Example 6). A combination of higher temperature and lower space velocity in reactor C (even at end of run conditions in reactors A and B) produced even higher saturates, 96.2%. For a 100N feed stock, end-of-run product with greater than 90% saturates may be obtained with reactor C operating as low as 290 C. at 2.5 v / v / h (Table 3).

2 TABLE 2 SOR EOR EOR EOR Re- T LHSV T LHSV T LHSV T LHSV actor (...

example 3

[0072] The effect of temperature and pressure on the concentration of saturates (dewaxed oil) at constant VI is shown in this example for processing the under extracted 250N raffinate feed. Dewaxed product saturates equilibrium plots (FIG. 5) were obtained at 600, 1200 and 1800 psig (4.24, 8.38 and 12.5 mPa) H2 pressure. Process conditions were 0.7 LHSV (reactor A+B) and 1200 to 2400 SCF / B (214 to 427 m.sup.3 / m.sup.3). Both reactors A and B were operating at the same temperature (in the range 350 to 415.degree. C.).

[0073] As can be seen from the figure it is not possible to achieve 90 wt. % saturates at 600 psig (4.14 mPa) hydrogen partial pressure. While in theory, one could reduce the temperature to reach the 90 wt. % target, the space velocity would be impracticably low. The minimum pressure to achieve the 90 wt. % at reasonable space velocities is about 1000 psig (7.0 mPa). Increasing the pressure increases the temperature range which may be used in the first two reactors (react...

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Abstract

A process for producing a lubricating oil basestock having at least 90 wt. % saturates and a VI of at least 105 by selectively hydroconverting a raffinate from a solvent extraction zone in a two step hydroconversion zone followed by a hydrofinishing zone, and a lubricating oil basestock produced by said process.

Description

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.FIELD OF THE INVENTION[0002] This invention relates to lubricating oil basestocks and to a process for preparing lubricating oil basestocks having a high saturates content, high viscosity indices and low volatilities.BACKGROUND OF THE INVENTION[0003] It is well known to produce lubricating oil basestocks by solvent refining. In the conventional process, crude oils are fractionated under atmospheric pressure to produce atmospheric resids which are further fractionated under vacuum. Select distillate fractions are then optionally deasphalted and solvent extracted to produce a paraffin rich ...

Claims

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Application Information

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Patent Type & Authority Applications(United States)
IPC IPC(8): C10G65/04C10G65/12C10G67/04
CPCC10G65/04C10G65/12C10G2400/10C10G67/0445C10G67/0418
Inventor CODY, IAN A.MURPHY, WILLIAM J.GALLAGHER, JOHN E.BOYLE, JOSEPH P.ZINICOLA, ANNE M.MAY, CHRISTOPHER J.KIM, JEENOK T.GROETSCH, JOHN A.HANTZER, SYLVAIN S.
Owner CODY IAN A
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