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The present invention relates to rκ:n-carcinogenic bright stock extracts and deasphalted oils and to a process for the production thereof.

In the refining of lubricant base stocks, a series of generally subtractive processes is employed to remove undesirable ccnponents from the process feed-stock. The most important of these processes include atmospheric and vacuum distillation, deasphalting, solvent extraction and de axing. These processes are basically physical separation processes in the sense that if all the separated fractions were recombined it would reconstitute the crude oil.

Refneries do not manufacture a single lube base stock but rather process several distillate fractions and a vacuum residuum fraction. Generally, at least three distillate fractions differing in boiling range, and the residuum, may be refined. These four fractions have acquired various names in the refining art, the most volatile distillate fraction often being referred to as the "light neutral" fraction or oil. The other distillates are called "intermediate neutral" and "heavy neutral" oils.

The vacuum residuum, after deasphalting, solvent extraction and dewaxing, is cx- monly referred to as "bright stock". Thus, the manufacture of lubricant base stocks involves a process for producing a slate of base stocks, which slate includes at least one refined distillate and one bright stock. Additionally, each subtractive step produces a byproduct which may be processed further or sold to an industry which has developed a use for the byproduct.

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Conventional processing of crude petroleum oil to recover fractions suitable for upgrading in various refinery processing operations employs multi-stage distillation. Crude oil is first distilled or fractionated in an atjoocspheric distillation tower, with residual m-rteria from the bottαn of the distillation tower being further separated in a vacuum distillation tower. In this (xπtoination operation, gas and gasoline generally are recovered as overhead products of the atmospheric distillation tcwer, heavy naphtha, kerosene and gas oils are taken off as distillate side streams and the residual material is recovered from the bottom of the tower as reduced crude. Steam may be introduced to the bottom of the tcwer and various side strippers used to remove light material from withdrawn heavier liquid products. The residual bottoms fraction or reduced crude is usually charged to a vacuum distillation tcwer. The vacuum distillation step in lube refilling provides one αr more raw stocks within the boiling range of about 550°F (288°C) to 1050°F (566°C), as well as the vacuum residuum byproduct. Often the vacuum charge is heated by a furnace means in order to vaporize a portion of the charge. The preheated charge normally enters a lower portion of the vacuum tcwer and the vapors therefrom rise t±rough the tcwer where they are cooled in selected stages producing successively lighter liquids which are separately withdrawn as the sidestream raw stock products. In lube refining, excess liquid runback, known as σverflash material, may be cmbined with the vacuum residuum and either wit-hdrawn from the tcwer or charged to a deasphalting unit far further processing ar dealt with in other cxnveπtional ways known to those skilled in the art. The σverflash material may alternatively be withdrawn, recovered and charged directly to a solvent extraction unit. The presence of metallic impurities, asphaltenes and the like may render this material unsuitable far this step or likewise, far a catalytic processing step. Typical vacuum distillation systems are disclosed in U.S. Patent Nos. 2713023, 3886062, 4239618 and 4 261814. Vacuum tower designs particularly germane to the present invention are disclosed in U.S. Patent Nos. 3929626 and 3989616.

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Following vacuum distillation, each raw stock is extracted with a solvent, e.g. furfural, phenol αr chlorex, which is selective for aromatic hydrot-sarbons, removing undesirable coπponents. The vacuum residuum usually requires an additional step, typically propane deasphalting, to remove asphaltic material prior to solvent extraction. The products produced far further processing into base stocks are known as raffinates. The raffinate from solvent refining is thereafter dewaxed by admixing with a solvent such as a blend of methyl ethyl ketαne and toluene, for example and then processed into finished base stocks.

The solvent extraction step separates hydrocarbon mixtures into two phases; the previously described raffinate phase which contains substances of relatively high hydrogen to carbon ratio, often called paraffinic type materials, and an extract phase which contains substances of relatively low hydrogen to carbon ratio often called aromatic type materials. Solvent extraction is possible because different liquid ccπpσunds have different solution affinities for each other and seme ∞πibinations are completely iscible while other x-mbinaticns are almost inmiscible. The ability to distinguish between high carbon to hydrogen aromatic type and low carbon to hydrogen or paraffin type materials is termed selectivity. The mere finely this distinguishing can be done the higher the selectivity of the solvent.

Furfural is typical of a suitable solvent extraction agent. Its miscibility characteristics and physical properties permit use with both highly aromatic and higher paraffinic oils of wide boiling range. Diesel fuels and light and heavy lubricating stocks are refined with furfural. Furfural exhibits good selectivity at elevated t_eιtperatures (175-250°F (79-121°C)) . In a typical furfural solvent extraction unit for lubricating oils, the raw feed is introduced below αr about at the center of the extraction tcwer. Furfural is fed into the top or upper portion of the tcwer. Recycled extract may be introduced

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into the lower section of the tower as reflux. likewise, internal reflux is effected in the tcwer fcy the t-eπperature gradient which is brought about by introducing the solvent at an elevated t_exDperature and by intermediate cooling systems. Furfural solvent is recovered from the raffinate and extract phase streams αr layers in suitable distillation and stripping equipment. The stripped and recovered solvent is then recycled.

While the furfural solvent extraction unit raffinate goes on to further processing, the extract frcαt the operation often finds utility in a broad range of industrial applications. Applications for these arαπαatic extracts often vary according to the particular properties of the extracts, these properties being largely a function of the feedstock used and unit conditions. Far example, as described in "A New Look at Oils in Rubber" by H.F. Weindel and R.R. Terc, Rubber World. r.tecember, 1977, these extracts often find further ^• utility as low and high viscosity aromatic extender oils for rubber processing. Bright stock extracts (BSE), obtained by solvent- refining deasphalted vacuum resids during the production of bright stocks, are useful in rubber processing and find utility as ink oils as well. Like the lighter aromatic extracts, BSE's possess excellent solvent characteristics which lend -themselves to great potential utility.

Besides having utility as a feedstock to the solvent extraction unit, the raffinate stream of the deasphalting unit can find further utility as a speciality oil. Depending an its characteristics, this stream, also known as deasphalted oil (DAO), can find utility as an extender oil for rubber processing, an ink oil, etc.

In recent years, α-xncerns have arisen regarding the potential hazards associated with the use of various aromatic oils, DAO's and BSE's. As noted in U.S. Patent 4 321 094, at col. 2, lines 9-14, "... many printing ink oils still contain prcportiαns of aromatic hydrocarbons

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which either are proven to be carcinogenic, such as benzene, or are believed to be carcinogenic, such as toluene and polycyclic cxxπpσunds. Clearly elimination of these from an ink would be desirable far health reasons". As a result of these concerns, many refiners are no longer willing to supply DAO's or aromatic extracts, including BSE's, far these speciality applications. Those refiners that continue to market these products must provide labels outlining the potential risks associated with the use of these products. This has lead to the development and selection of alternate materials for applications previously fulfilled by DAO's and BSE's, as evidenced by U.S. Patent Nos. 4 321094 and 4 519841. The use of these alternative solvents often carried with it the penalty of higher costs and inferior finished product quality.

To determine the relative carcinogenic activity of a deasphalte oil or an aromatic extract such as a BSE, a reliable test method far assaying such activity in ccπplex hydrocarbon mixtures is required. A highly reproducible method showing strong cαrrelatiαn with the carcinogenic activity index of hydrocarbon mixtures is disclosed in U.S. Patent No. 4499187. From the testing of hydrocarbon samples as disclosed in U.S. Patent No. 4 499 187, a property of the sample, known as its Mutagenicity Index (MI) is determined. Hydrocarbon mixtures exhibiting Mi's less than or equal to 1.0 are known to be ncαi-carcinogenic, while samples exhibit-ing Mi's equal to about 0.0 are known to be completely free of mutagenic activity. It would be desirable to produce deasphalted oils and/or aromatic extracts such as bright stock extracts which are nc-n-carcinogenic such that contact with same will not cause the development of cancerous growths in living tissue. It would be still more desirable to produce DAO's and/or BSE's which are free of mutagenic activity; that is, that contact with such products would not induce mutations in DNA and in living cells.

In broad terms the invention provides a process for preparing bright stock extract or deasphalted oil which is either substantially non-

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carginogenic αr is substantially free from mutagenic ac-tivity. The invention also provides bright stock extract αr deasphalted oil which is either substantially ncai-carcinogenic αr is substantially free of mutagenic activity. In accordance with the present invention, a ncinrcarcinogenic bright stock extract and a nca-carcincgenic deasphalted oil are provided, as well as processes far their production from reduced hydrocarbon c-rude feedstocks. The process for the procluction of the nαn-carcinogenic bright stock extract (BSE) from a reduced hydrocarbon crude feedstock cαπprises establishing a fimcticnal relationship, preferably by regression, between mitagenicity index (MI) and a physical property indicative of iαitagenicity far a bright stock extract stream. From this relationship, a critical physical property level is determined which, when achieved, the resultant BSE exhibits an MI less than αr equal to 1.0. Process conditiαns are established to consistently achieve the desired BSE physical property level. Reduced feedstock is then fed into a vacuum distillation column wherein the feedstock is separated into at least one product of distillation and a residuum byproduct. Next, at least a fraction of the residuum is fed into a selective solvent deasphalting unit to produce a deasphalted raffinate and an asphaltenic or tar extract. Then, at least a fraction of the deasphalted raffinate is passed through at least one solvent extraction step to reduce the deasphalted raffinate's aromatic content and to produce a bright stock raffinate and a bright stock extract, the bright stock extract having an MI less than αr equal to about 1.0. The BSE so produced is substantially non-carcinogenic.

The invention can also provide a BSE substantially free from mutagenic activity. The 5% distillation boiling point has been found to be a particularly preferred physical prcperty of the BSE for correlation with ME.

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The process for the production of the non-carcinogenic deasphalted oil (DAD) comprises establishing a functional relationship, preferably by regression, between mutagenicity index (MI) and a physical property indicative of mutagenicity far a deasphalted oil stream. From this relationship, a critical physical property level is determined which, when achieved, the resultant DAO exhibits an MI less than or equal to 1.0. Process conditions are establishe to consistently achieve the desired DAD physical property level. Reduced feedstock is then fed into a vacuum distillation column wherein the feedstock is separated into at least one product of distillation and a residuum byproduct. Next, at least a fraction of the residuum is fed into a selective solvent deasphalting unit to produce a deasphalted oil and an asphaltenic αr tax extract, the DAO having an MI less than αr equal to about 1.0. The DAO so produced is substantially nαn-carcinogenic.

The invention can also provide a DAO substantially free from mutagenic activity, as well as a process far producing same.

The 5% distillation boiling point is believed to be a particularly preferred physical property of the DAO for correlation with MI.

When the MI is selected to be less than one, then the critical property will be the physical property which yields a value of MI substantially equal to 1.0.

When the MI is selected to be substantially zero, then the critical property will be the physical property which yields a value of MI substantially equal to zero.

Reference is now made to the aαxβ&panying drawings in which:

Fig. 1 is a partial lubricant refinery configuration schematically representing the steps of vacuum distillation, deasphalting and solvent extraction, wherein a blended overflash and vacuum residuum feed to a deasphalting unit is utilized.

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Fig. 2 is a partial lubricant refinery configuration schematically repα^senting the steps of vacuum distillation, deasphalting and solvent extraction wherein a straight vacuum residuum feed to a deasphalting unit is utilized.

Fig. 3 is a graph shewing the relationship between Mutagenicity index, as determined by a Modified Ames Assay, and the 5% boiling point far 19 BSE's produced in Refinery A.

Fig. 4 is a graph shewing the relationship between Mutagenicity Index, as determined by a Modified Ames Assay, and the 5% boiling point for 5 BSE's produced by Refinery B.

Any lubricant refinery which utilises a solvent extraction step and/or a deasphalting step in the production of bright stocks is cαπteπplated far use herein. The process of this invention will now be described with reference to Figure 1, which schematically depicts a particularly preferred lubricant refinery partial configuration. A suitable reduced crude prepared by atmospheric pressure distillation of a paraffin base αr other suitable base crude oil is passed via line 1 to crude unit vacuum distillation tower 2. Light ends are removed from the system via line 3. A light distillate fraction, which is a raw lubricant stock, known as light neutral oil, is passed from tower 2 via line 4 either to a storage tank, not shown, or to the solvent extraction unit 22 for further processing. Similarly, an iiϊtermediate neutral oil is passed via line 5, and a heavy neutral oil is passed via line 6, either to storage tanks (not shown) or to solvent extraction unit 22. An σverflash boiling range material, is wit-hdrawn from conduit 7 located at a lower portion of the vacuum tower 2 above the reduced crude inlet txnduit 1. Vacuum tower residuum is withdrawn from conduit 10. A pαrtion of the vacuum tower residuum withdrawn from conduit 10 is withdrawn by conduit 12 and a portion of the overflash material withdrawn by conduit 7 is withdrawn by conduit 9. These portions are wit-hdrawn and cx-mbined in conduit 13 and passed to deasphalting unit 15, where it is treated by any of a

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number of useful processes, such as propane deasphalting (PDA), which is particularly preferred. The σverflash material not withdrawn by conduit 9 far cab ing with the residuum is withdrawn by conduit 18 and may be stored in a storage tank, not shown, or solvent treated in extraction unit 22. The residuum not withdrawn by conduit 12 will pass t-hrough conduit 14 and may be stored in a storage tank (not shown) or processed further as desired. Upon deasphalting, the deasphalted oil product, αr raffinate, is withdrawn t-hrough conduit 16 and, either sent far further processing into bright stock or withdrawn and stored as DAO via conduit 26. The extract αr tar from the deasphalting step is withdrawn through conduit 17. If bright stocks are to be produced, at a suitable point in time, the deasphalted oil raffinate is passed to the solvent extraction unit 22 through conduit 16 where it is treated with any one of a number of suitable solvents to remove undesirable constituents by preferential solution to produce a lubricant bright stock raffinate. The bright stock raffinate so produced is passed via conduit 23 and the bright stock extract removed via conduit 24. As mentioned, in the extraction unit 22, any suitable selective solvent may be used, such as furfural, phenol, chlαrex, nitioberώene, with furfural being a particularly preferred solvent. At an appropriate point in time, -the flow from conduit 16 is halted and from either conduit 4, 5 αr 6 substituted therefor. The extraction unit will again remove the unwanted aromatic compounds and the light (100 SUS) , intermediate (300 SUS) or heavy (700 SUS) neutral oil raffinate so produced, removed via conduit 19, 20 or 21, respectively. The raffinates processed by the solvent extraction unit are dewaxed using any suitable process or stared in storage tanks (not shown) for later processing.

It will be recognized by those skilled in the art that the process stages described above are conventional. The illustration chosen shows the preparation of four segregated base stocks, but of course fewer or more distillate fractions may be prepared. With certain

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highly paraffinic raffinates, which are substantially free of asphalt, treatment in the deasphalting unit 15 may be omitted. In other cases, unit 15 may provide a combined deasphalting and solvent extraction process. These and other variants are contemplated as within the scope of the present invention, the variations not being of material significance. It will be further recognized by those skilled in the art that the process being described is a blocked-out operation, but that variants thereof which would provide continuous flow of a deasphalted raffinate, for example, via line 16 to a dedicated extraction unit (not shown) and thence via conduit 23 to a storage tank αr dewaxing unit (both not shown) , are contemplated as within the scope of the present invention.

Depending upon whether the production of nctn-carcinogenic bright stock extract or ncnrcarcinogenic deasphalted oil is desired, samples are withdrawn frc either conduit 24 (for the bright stock extract) or conduit 26 (far the deasphalted oil) during preliminary runs, or from storage tanks (not shown) where previously collected samples reside. It can be beneficial to note the processing conditions responsible for producing a particular sample. Iitipαrtaπt parameters may include, but are not limited to: 1) percent of overflash material blende with crude unit vacuum tower residuum for charging the deasphalting unit; 2) the heavy-neutral distillate cut point; 3) other vacuum tower operating parameters such as steam inlet teπperature, flashing zone absolute pressure and other internals; 4) deasphalting unit operating conditions, such as solvent treatment rate; 5) solvent extraction unit charge properties, such as whether blends of other streams are charged to the unit together with the deasphalted raffinate; and 6) solvent extraction unit operating conditions such as solvent treatment rate. thαugh not found to influence the production of the DAO's and BSE's of this invention, another variable worthy of note may be the crude or crude blend charged to the atmospheric distillation unit for producing the reduced crude charged to the crude unit vacuum distillation tcwer.

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lt has been discovered that polynuclear aromatic compounds (PAC) of 3-7 rings are responsible for the mutagenic/carcinogenic activity of DAO's and BSE's. These biologically active PAC are generally considered to fall in the boiling range of 640 to 1000°F (338 to 538°C) . Unfortunately, suitable methods for reliably detecting these PAC in deasphalted oil or bright stock extract-type materials do not exist. It has been found, however, that the distillation properties of a DAO αr a BSE, in particular, the 5% boiling point, can provide a process parameter indicative of the relative mutagenicity/ carcinogenicity of a particular DAO αr BSE process stream. Also, the initial boiling point (IBP) of the DAO αr BSE has been found to provide another useful process parameter indicative of relative mutagenicity/carcinogenicity.

The bright stock extract αr deasphalted oil samples collected are distilled using a standard method, such as ASTM D-1160, with preferably, at least the 5% boiling point (HP) recorded for each sample. Each sample is also tested to determine its relative mutagenicity. The Modified Ames Assay procedure disclosed in U.S. Patent 4 499 187 is particularly preferred as it can rapidly and reliably determine the potential carcinogenic activity of hydrocarbon mixtures of petroleum origin. Mutagenicity index data obtained from the Modified Ames tests and 5% HP data obtained from distillation tests are regressed using well-known simple linear regression techniques to develop a linear relationship between these parameters characteristic of that refinery's basic operation. Mutagenicity index (MI) , as disclosed in U.S. Patent 4499187, is a ranking for relative mutagenic potential. MI is the slope of the dose response curve for mutagenesis. An example of such a regression line is shown in Figure 3. Since ncxnrcarcincgenic oils are known to exhibit Mi's of less than or equal to 1.0, the 5% BP which yields a value of MI = 1.0 is determined from the regression relationship and selected as a "critical" 5% BP. Process conditions selected to produce a DAD and/or

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a BSE (as desired) having a 5% BP at or above the critical 5% BP value will be non-t-arσinogenic. As may be seen from the regression relationship of Figure 3, BSE's can also be produced having no mutagenic activity at all when they are produced to have a 5% BP at or above the point where ME = 0. likewise, DAO's free from mutagenic activity can also be produced in the same manner.

Reference is again made to Figure 1. zAs mentioned, to achieve a DAO and/cr a BSE having a 5% BP at αr above the critical value, processing alterations will probably be required. One alteration found to influence the distillation characteristics of the resultant DAO or BSE is the amount of σverflash material blended with the vacuum residuum for charging the deasphalting unit 15. Should the lube refining process of Figure 1 be present, the settings of valves 8 and/or 11, should they be present, could be varied to reduce the percentage of overflash material charged to the deasphalting unit. While the use of an overflash/residuum blend as a deasphalting unit charge is desirable from the standpoint that it increases the amount of bright stock produced while also producing bright stocks of somewhat lower viscosity, its use can now be optimized so that substantially non- carcinogenic deasphalted oils and/cr bright stock extracts are also produced.

It is important to recognize that the process of this invention is not limited to the lube refining processes depicted in Figure 1 and explained above. Another partial lubricant refinery configuration useful in the practice of this invention is depicted in Figure 2. The configuration shown in Figure 2 is similar to that of Figure 1, with the exception that no overflash side-draw is present for removal and blending with residuum for charging to the deasphalting unit 15. The process for producing a non-carcinogenic DAD or BSE would be carried out as described above, with the exception that no ability to alter the 5% BP of the end-product by varying the percentage of

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σverflash charged to the deasphalting unit would exist. Other process condition alterations, such as those described above or others known to those possessing ordinary skill in the art would be required and are envisaged as useful in the practice of this invention.

The invention is illustrated by the following examples.

In accordance with the process previously described, nineteen bright stock extracts were produced under varied process conditions at Refinery A, using various input crude blends, with representative samples of each taken. Mutagenicity tests were conducted using the Modified Ames Assay procedure previously referred to with two additional modifications. These were: a higher dose range (10 - 80 rather than the standard 5 - 50 μl/plate) was employed, in keeping with the lower mutagenicity of these materials relative to that observed for typical vacuum distillates, the amount of sample extracted for testing was 2 grams rather than the 2 ml used for less viscous materials. Distillation profiles were obtained for each sample using ASM D-1160. Data obtained are shewn in Table 1 below.

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Table 1

Properties of Bright Stock Extracts from Refinery A

Sample Mutagenicity 5% BP Number Index ° Description

1 3.1 Blended with heavy neutral extract; Viscosity = 69.7 cSt

2 2.0 Furfural treat: 300%; PDA treat: 600%

3 2.1 Contains overf]ash; IBP = 718°F

(381°C) ; viscosity = 70.6 cSt

4 1.6 Furfural treat: 370%; PDA treat 600%; crude source: 13% Clyde, 11%

Arab Light, 4% Beryl, 20% Statfjcrd,

52% Fulmar; IBP = 809°F (432°C) ; viscosity = 61.3 cSt

1.7 935 70% Statfjαrd, 30% Arab Litght; (502 ^β C) viscosity = 50.3 cSt

1.3 945 Furfural treat: 300%; PDA treat: (507°C) 600%; (.rude source: 76% Statfjord,

17% Beryl; 7% FUlmar; viscosity =

65.7 cSt

1.1 954 Furfural treat; 300%: PDA treat: (512°C) 600%; crude source 80-90% Fulmar,

10-20% Arab Light; viscosity 68.23 cSt

8 0.9 957 Furfural treat : 300%; PDA treat : (514°C) 600%; crude source: 54% Fulmar, 30%

Statfjord, 13% Clyde, 3% Arab Li«ght

0.8 947 Furfural treat: 300%; PDA treat: (508°C) 600%; crude source: Statfjord/

Fulmar; viscosity = 64.0 cSt

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0.6 Furfural treat: 300%; PDA treat:

600%; crude source: Statfjord/ Fulmar; viscosity = 65.4 cSt 0.6 Furfural treat: 300%; PDA treat:

600%; crude source: Statfjαrd/ F_ιlmar; viscosity = 66.0 cSt 0.6 Furfural treat: 300%; PDA treat:

600%; crude source: 85% Statfjord, 15% Fulmar; viscosity = 63.2 cSt 0.5 FUrfural treat: 300%; PDA treat: 600%; crude source: 52% Statfjord,

33% Fulmar; 11% Clyde, 4% Arab light 0.0 968 Furfural treat: 300%; PDA treat:

(520°C) 600%, c-rude source: 52% Statfjord, 33% Falmar; 11% Clyde, 4% Arab Light 0.4 939 From North Sea crude; viscosity =

(504°C) 68 cst 0.4 ^" 958 Viscosity = 70.3 CSt

(515°C) 0.4 962 Furfural treat: 350%; PDA treat:

(517°C) 600%, crude source: 59% Statfjord, 18% Beryl, 15% Fulmar, 4% Clyde, 4% Arab Light 0.3 968 Furfural treat: 350%; PDA treat:

(520°C) 600%, crude source: 59% Statfjord, 18% Beryl, 15% FUlmar, 4% Clyde, 4% Arab Hght 0.0 973 Furfural treat: 370%; PDA treat:

(523°C) 600%, crude source: 2% Clyde, 2% Arab Light, 13% Beryl, 79% Statfjord, 4% Ful_mar; IBP = 873°F (467°C); viscosity = 54.5 cSt

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The 5% BP and MI data were linearly regressed using well-known techniques to determine the relationship between those variables. The results of this regression are shown in Figure 3. As shewn in Figure 3, excellent correlation was established, with a correlation coefficient, r, of 0.92 found. The critical 5% BP (MI=1) was found to be about 945°F (507°C) for Refinery A. Additionally, from this relationship, it can be seen that a BSE having substantially no mutagenic activity (MI=0) should be produced when the 5% BP exceeds about 978°F (526°C) .

Khcwing the critical 5% BP required to produce a substantially non- carcinogenic BSE, process conditions can be established, as one skilled in the art would recognize, to achieve BSE production cx-nsistently having a 5% BP at or above the critical value. Non- carcinogenic bright stock extract can then be produced using the processes previously described. Following these process steps will result in the non-carcinogenic BSE of this invention.

At Refinery B, five bright stock extracts were produced under varied process conditions and sampled. As in Example 1, MI and 5% BP were determined for each sample. These data are shewn belσw in Table 2.

Table 2

Properties of Bright Stock Extracts from Refinery B

Sample Description

BSE, viscosity = 70.3 cSt BSE, viscosity = 70.3 cSt BSE, viscosity = 70.3 cSt BSE, viscosity = 70.3 cSt BSE, viscosity = 70.3 cSt

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The 5% BP and ME data were linearly regressed to determine the relationship characteristic of Refinery B. The results of this regression are shown in Figure 4. Again, excellent correlation is achieved, with an r value of 0.88 found. The critical 5% HP was found to be about 925°F (496°C) for Refinery B. Again, as at Refinery A, a BSE substantially free from mutagenic activity should be produced when the 5% BP exceeds about 978°F (526°C) .

Using the knowledge of one skilled in the art, Refinery B's process conditions can be adjusted to achieve BSE production consistently having 5% BP's at αr above the critical value of 925°F (496°C) .

The bright stock extract can then be produced in the manner previously described. By following these process steps non-carcinogenic BSE's can be produced.

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At a lubricant refinery configured substantially as depicted in Figure 1, ten deasphalted oils are produced under varied process conditions during trial runs and sampled. As in Examples 1 and 2, MI and 5% BP are determined from the regression relationship so obtained.

Using the knowledge of one skilled in the art, refinery process conditions are adjusted to achieve DAO production consistently having 5% BP's at or above the critical value. The deasphalted oil can then be produced in the manner previously described. By following these process steps non-carcαncgenic DAO's are produced.

t-hough the present invention has been described with preferred embodiiαents, it is to be understood that modifications and variations may be utilized within the scope of the appended claims.

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