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Publication numberUS2886523 A
Publication typeGrant
Publication dateMay 12, 1959
Filing dateApr 25, 1955
Priority dateApr 25, 1955
Publication numberUS 2886523 A, US 2886523A, US-A-2886523, US2886523 A, US2886523A
InventorsClaridge Elmond L, Wallin John M
Original AssigneeShell Dev
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Lubricating oil refining process
US 2886523 A
Abstract  available in
Previous page
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Claims  available in
Description  (OCR text may contain errors)

y 1959 E. CLARIDGE ETAL 2,886,523



Pasadena, Calif., assignors to Shell Development Company, New York, N.Y., a corporation of Delaware Application April 25, 1955, Serial No. 503,811 2 Claims. (Cl. 208-312) This invention relates to a process for the refining of petroleum oils. It relates more particularly to an improved process for the production of lubricating oils, of catalytic cracking feed stocks and products therefrom, and ofaromatic oils. g 1

The usual practice in the art of catalytic cracking of petroleumoils to' produce motor fuels is to recover the higher boiling components from a crude oiltas distillate, catalytically crack this disillate feed stock jt o produce lighter hydrocarbons therefrom, fractionate the total product to separate the useful fractions, and to recycle the heavier material to the catalytic cracking step to increase the yield oflighter material or to subject it to a thermal cracking. A substantial portion of this heavier fraction is highly refractory to catalytic cracking, that its recycle is a burden on the cracking operation. On the other hand, it is generally considered to be uneconomical to separate the refractory components from the more reactive components. The use of this product as an aromatic oil has the drawback that it contains a substantial proportion of para fiinic material and heretofore it has been uneconomical to separate these components.

Other valuable products of petroleum refining are the various lubricating oil fractions. I These are normally produced by separating suitable high boiling fractions "as distillates from the oil, as by distillation under vacuum, to minimize thermal cracking. Mixtures of the desirable lubricating oil components are usually recovered from the distillates by an extraction process, such as by physical contacting with a suitable selective solvent for the arornatic components; solvents such as phenol, cresols, furfural, nitrobenzene, and the like are used for this purpose. However, an attempt to separate all of the desirable components from the undesirable ones is not practical by solvent extraction because of the wide variety of typesof compounds present. As a consequence, a compromise is usually required. Y .Maximum recovery of the desirable lubricating oil components as rafiinate oil requires separation therewith of a portion of undesirable components, which are of a more or less aromatic character and of lower viscosity index. This, of course, lowers the viscosity index-of the raffinate oil. On the other hand, in order to produce a raffinate having a high viscosity index, a' morecomplete rejection of the aromatic hydrocarbons must be made and this results also in a rejection (extrac tion) of a substantial proportion v,of components which would otherwise be desirable raflinate components.v :It is, therefore, a principal object of the present inven tion to provide an'improved'process for the "refining of petroleum oils. improved process for the catalytic cracking of petroleum oils and for the solvent extraction of lubricating oil petroleum stocks. Theseobjects will be better understood and others will be apparent from the detailed descriptionof the invention, taken in conjunction with the drawing which is Ea schematic sketch of a system suitable for the production of a lubricating oil material in accordance with, the process of the invention.

A more specific object is provide an 2,886,523 Patented May 12, 1959.

It has now been found that catalytically cracked heavy gas oil is advantageously and economically separable into paraflinic and aromatic fractions, by extraction with a selective solvent extract phase from a solvent extraction of a lubricating oil stock containing paraffinic, naphthenic and aromatic components, with the recovery in a raflinate phase from this extraction of a mixture of parafiinic com: ponents derived from both the lubricating oil stock and the} catalytically cracked gas oil and recovery in an extract of; aromatic components also derived from both sources. The major proportion of the heavy gas oil components will, in general, have boiling points of at least about 500". F., and preferably at least about 550 F., with the,50% boiling point ranging from about 550 F. to about 800. F., while the end boiling point may be as high as 1000 to. 1100 F.

In accordance with one aspect of the invention, the resulting raffinate is separated, as by distillation, into: higher and lower molecular weight fractions and the:v higher molecular weight fraction is combined with the rafiinate from the extraction of the lubricating oil. stock. The lower molecular weight components, although of lower viscosity, exhibit excellent oxidation-stability prop erties and excellent additive response, so that their incorporation in the total lubricating oil rafiinate gives an oil. of improved stability characteristics. In another aspect of the invention,-the recovered aromatics mixture is fracf tionally distilled to produce a lower boiling fraction, corn prising aromatics from the catalytically cracked gas oil, and-'a higher boiling fraction comprising aromatics from the lubricating oil fraction and the higher boiling fraction. is combined with the residual material from the catalytic cracking feed preparation to produce a suitable residual fuel oil. we l Another aspect of the invention is based upon the fact that the catalytically cracked oil contains only a relatively;

small proportion of monocyclic aromatic hydrocarbons, which are desirable components in substantial proportion in motor lubricating oil, thus giving by ordinary solvent extraction a raftinate oil which is deficient in certain desired properties. On the other hand, in order to produce from a virgin lubricating oil stock an oil having suitable viscosity characteristics, it is usually necessary to eifect the separation, as bysolvent extraction, between paraffinic and aromatic components in such a manner as to remove desirable saturate components as well as desirable aromatic components in the extract phase. 7

.Now, because of the low monocyclic aromatics content of the catalytic oil and the relatively high concentration of them in the extract phase from the extraction of the virgin stock, extraction of the catalytic oil with said extract phase results in the transfer of an effective amount of the monocyclic aromatics tothe raflinate phase in this second extraction. These monocyclic aromatics are dc sirable in the raffinate whether it is to be utilized as a motor lubricant or as a catalytic cracking feed stock. I 'As lubricant components, they impart cleanliness characteristics to the oil,'reducing ring-sticking and carbon deposition. As catalytic cracking feed, they give rise to aliphatic and aromatic gasoline components.

The single drawing provides a fiow diagram of the process of the invention when utilized to produce a lubricating oil material of improved properties. There a stream {of a virgin lubricating oil stock is admitted through a line 10 to the bottom of an extraction zone 12. The lubricating oil stock passes .in countercurrent flow to a solvent selective for aromatic hydrocarbons which is admitted to the other end of the zone via a line 13. An extract solution containing nearly all of the polycyclic aromatics and resins and a large portion of the monocyclic aromatics is removed from the bottom of the zone in a conduit 15. A

primary rafiinate enriched in paraflinic hydrocarbon leaves aeaaees 3 the extraction zone 12 through a line 16. The extract solution is passed to a second extraction zone 18 wherein it is employed as the extractive solvent for the treatment of a heavy catalytically cracked gas oil admitted to the bottom of that zone via a line 20. A second raflinate enriched in paraffinic hydrocarbons and containing a large portion of the monocyclic aromatic hydrocarbons present in this second extraction system leaves from the top of the zone 18 via a line 22. The aromatic enriched extract phase is removed from the bottom of the zone in a conduit 23 and is introduced to a central portion of a solvent stripper 25. In the latter vessel the aromatics are removed overhead, leaving through a line 27. Stripped solvent returns to the first extraction zone through the aforementioned line 13. At least a portion of the second raflinate carried by line 22 is blended with the primary raffinate from the first extraction zone to obtain a blended product of greater oxidative stability and enhance monocyclic aromatic content compared to the oxidative stability and monocyclic aromatic content of the primary raffinate.

, When the rafiinate is to be utilized as a lubricating oil, it can be dewaxed, as desired, by the usual dewaxing methods, as by. solvent dewaxing. However, as a catalytic cracking feed stock, the waxy hydrocarbons present, whether originating from the lube stock or the cat-cracked gas oil, or both, represent desirable cracking stock.

The relatively low content of monocyclic aromatic components in a heavy catalytically cracked gas oil is illustrated by the data in Table I, obtained by an examination of such an oil from a commercial refinery operation. The oil, containing a small amount of catalyst fines carried over from the catalytic cracking, generally referred to as catcracked slurry oil, was sampled under normal operating conditions of approximately 31,000 barrels per day feed to the catalytic cracking unit. The composite feed to the catalytic cracker had an API gravity of 282 at 60 F. and the following distillation characteristics: initial boiling point (I.B.P.), 385 F.; 10% over at 556 F.; 50% over at 710 F.; 90% over at 883 F. and an end boiling point of 1000 F.; the pour point was 80 F.

Table I.--Catalytically cracked slurry oil (a) General properties:

(1) API gravity- (2) 'Pour point, 1L +90 (b) Hydrocarbon type analysis (by isopentane deasphaltiug and alumina and silica gel chromatography):

(c) Properties of saturates of b(4):

(1) m 14 (3) Specific dispersion at 90 F (4) Pour point. F (5) Yield of 0 F. pour point, oil, percent w (6) Viscosity data on 12 F. pour int oil:

Vise. at 100 F., (s Visc. at 210 F., 05.. Viscosity index (7) Viscosity index of 0 F. pour poin o (8) Yield of deoiled wax at +25 F., and oil/solvent ratio of 1:3 (MEK, toluene, benzene commercial Dewaxing Solvent). percent w 21. (9) Melting point of Wax, F 142 (mol wt. =460 46). (10) Penetration of wax 1.9 mm. (100 g., 5 sec. C.). (11) Normal parat'fins by urea extrac- 27.0 (10.2% w. of gas oil).

.4301. 0.797 (API 43.4 at F.).

(25% w. on gas oil).

22.66 (109 Saybolt). 4.54. 131.

tion, percent w. of saturates ((1)-Properties of polycyclics trom l.(6):

' (1)'Pour point, F 30 (2) Density (90/4)-- 028 (3) Viscosity:

, Analysis of another catalytically cracked slurry oil, obtained from a different refinery catalytic cracking unit, by conventional silica gel adsorption techniques, with 5% benzene in petroleum ether and acetone as eluting agent for the adsorbed hydrocarbons, gave, on a deasphalted and deresined basis, 41% paraifins and naphthenes (saturates) and 50% aromatics. Dispersion data indicated the aromatics to be composed of about 5%.monocyclics, 2% dicyclics, tricyclics and 23% tetracyclics.

The heavy catalytically cracked gas oil, produced in the sarneunit while producing the slurry oil characterized in Table I, had an API gravity of 29.1 and initial and final boiling points of about 465 F. and 660 F., respectively. Further inspection gave the characteristics tabulated in Table II.

T able Il.-Heavy catalytically cracked gas oil Percent Moi wt.

Although a small proportion of this heavy cat-cracked gas oil (HCCGO) is recycled to the cat-cracking operation because of its non-aromatic content, it is not a desirable feed to the cat-cracked unit because of the cokeforming polyaromatics and polar substances, so that most of it is usually used as feed to a thermal cracking process. It has not heretofore been found to be economically feasible on a large scale to separate the non-aromatics from the aromatics to provide a more suitable catalytic cracking feed stock from this heavy gas oil.

Analyses are given in Table III for a lubricating oil distillate and the complementary rafiinate and extract obtained in a plant scale countercurrent solvent extraction with phenol as selective solvent. The distillate (ET 250 distillate) was a vacuum distillation fraction of an East Texas crude, selected to yield, upon extraction and dewaxing, a lubricating oil having a viscosity of 250 SUS at The quantity and viscosity index of the saturates in the extracts and raflinates obtained by solvent extracting three difierent high viscosity index lube crudes and one medium viscosity index lube crude (mixture) are given in TableIV.

Table l I V.---Solven t extraction 1 of lab distillates I ET, WTEand indicate, respectivelmyEast Texas, West Texas Ellenburger and Oklahoma City crudes.

Basis dewnxed distillate.

Furiural extraction.

d Phenol extraction. p

Processed by Duosol extraction with.propane-phenol-cresols solvent combination.

Although extract solutions from the extraction of different types of lube crude fractions are suitable in the practice of the invention, extract solutions resulting from the extraction of lube fractions to give high viscosity index (at least about 85) raflinates are particularly useful.

Extraction data are shown in Table V for extraction of a heavy cat-cracked gas oil with an HVI 250 extract solution. The extract solution was from plant extraction of an HVI (high viscosity index) 250 distillate (ET) to produce a 250 raffinate having a viscosity index of 88 (after dewaxing).

Table V.-S0lvent extraction of heavy cat-cracked gas oil with lube extract solution Run 1 2 3 Solvent 'loii ratio a 40 Raffinate, percent w. (basis HCCGO)- 74. 4 77. 8 64. 3 Sulfur, percent w 0.61 0.76 0. 53 Refractive index (70/D) 1. 4743 1. 4812 1. 4720 Density (70/4) 0. 8435 0. 8490 0. 8395 Extract:

Sulfur, percent w 1. 49 Refractive index (70/D) 1.5600 Density (70/4 0.9590 Total Recovery, percent w 90. 8

e Plant phenol extract solution: contained 13.3% w. of extract oil of do" 0.9553. 0.91% w. S.

* H0000: percent w. 5 1.12; no" 1.4890; d4" 0.8696.

Although the extract solution used as solvent was quite waxy at 25 C., the extracts obtained at all solvent to oil ratios were quite fluid at 25 C., indicating that the waxy components had been transferred to the rafiinate during extraction. The density of the extract in each case was greater than that of the extract obtained by stripping the phenol from the solvent extract solution and the density of the rafiinate in each case was lower than that of the original gas oil.

In order to demonstrate the utility of the present process for the preparation of catalytic cracking feed stock, catalytic cracking comparisons were made between (1) a West Texas vacuum flashed distillate (heavy flasher tops, the major portion of the catalytic cracking feed stock from which the heavy cat-cracked gas oil was derived), (2) a heavy cat-cracked gas oil (HCCGO), (3) a 250 extract from the extraction of an ET 250 distillate and (4) raffinates from the extraction of the I-ICCGO with the 250 extract solution. From the correlations obtained between (a) space velocity and conversion, (b) coke make and conversion, and to) gasoline make and conversion, significant illustrative data are available as shown in Table VI.

Table VII-Catalytic cracking comparisons I Conversion: percent v.=(pcrcent v. of 400 F.+gas oil). Space velocity: weight of oil per hour-per unit weight of catalyst.

- Yield of raflinate based on lICCGO.

a C4 to 400? F. gasoline, percent v.

similar conditions, there was an increase in conversion of approximately 9. units over that for the unextracted gas' oil. Although the conversion was essentially the same as for the extract, the coke make for the extracted gas oil was only about 50% (or less) of that for either the lube extract or the unextracted cat-cracked gas oil. Furthermore, at the same conversion of 55%, the gasoline yield was the same as for the flasher tops and about 40% greater than for either the lube extract or the cat-cracked gas oil. Gasoline yields at conversions ranging from about 33% cracked gas oil to be equivalent to the heavy flasher tops, while those for both the lube extract and the unextracted cat-cracked gas oil showed them to be substantially inferior. In some cases rafiinate yields of 100%, basis cat-cracked gas oil, of desirable cracking stock are obtainable.

Various lubricating oil extract solutions are suitable as extracting agent for the practice of the invention. Particularly suitable extract solutions are those obtained by extracting lubricating oil distillates to produce lubricating oil raffinates having a viscosity of at least about 200 SUS at 100 R, such as so-called 200, 250, 380 and heavy distillates. Expressed another way, the extract should comprise hydrocarbons having a molecular weight of at least about 300, preferably ranging from about 350 to about 500. However, extract solutions obtained in the production of so-called bright stock, by the solvent extraction of short residues, generally after deasphalting, where the molecular weights are of the order of 600 to 800, are suitable also.

Any of the usual and known selective solvents for the refinement of lubricating oils are suitable, such as furfural, phenol, nitrobenzene, sulfur dioxide, cresylic acids, sulfolane, and the like. The conditions of extraction are selected from those well known to the art and may be continuous or batchwise.

In order to demonstrate the utility of the process of this invention in the preparation of an improved lubricating oil, comparisons can be made between rafiinates obtained from a catalytically cracked heavy gas oil by extraction with (l) phenol in a typical phenol extraction process and (2) a phenol extract solution obtained by the extraction of a 250 ET distillate. Upon dewaxing the resulting rafiinates, and comparing them with respect to oxidation stability and susceptibility of the oil to additives, and also as to monocyclic aromatics content, it is found that the extraction of the cat-cracked heavy gas oil with the solvent-extract solution yields a superior raffinate product and that it has a higher content of monocyclic aromatic hydrocarbons than the other raflinate product.

We claim as our invention:

1. In a process for the production of a lubricating oil material from a heavy catalytically cracked gas oil and a virgin lubricating oil stock, the steps comprising (1) extracting the virgin lubricating oil stock with a solvent selective for aromatic hydrocarbons and separating an extract solution containing nearly all of the polycyclic aroto about 60% indicated the extracted catmatics and. resins and a large portion of, the monocyclic aromatics and. a primary raffinate enriched in paraffinic hydrocarbons, (2) extracting the cracked gas oil with said extract solution and separating a second rafiinate enriched in parafiinic hydrocarbons and containing a large portion of. the monocyclic aromatic hydrocarbons present in this second extraction system and (3) subsequently blending at least a portion of the second raffinate with the primary rafiinate to obtain a blended product of greater oxidative stability and enhanced monocyclic aromatic content compared to the oxidative stability and monocyclic aromatic content of the primary ratfinate.

2; A process in accordance with claim 1, wherein the heavy catalytically cracked gas oil contains a major proportion of components having boiling points of at least about 550 F., and the extract solution is the solution resulting from the selective solvent extraction of a lubricating oil distillate fraction in which the major proportion of the components have molecular weights of at least 8, 350 and the primary raflinate from the extraction'has a Viscosity index of at least about 85.

References Cited in the tile of this patent UNITED STATES PATENTS 2,139,392 Tijmstra Dec. 6, 1938 2,115,960 Lindeke May 3, 1938 2,155,745 Wagner Apr. 25, 1939 2,201,550 Van Dijck et al May 21, 1940 2,228,510 Dearborn et al. .4 Jan. 14, 1941 2,234,549 Bray Mar. 11, 1941 2,270,827 Tijmstra n Jan. 20, 1942 2,279,550 Benedict et al. Apr. 14, 1942 2,304,289 Tongberg' Dec. 8, 1942 2,342,888 Nysewander et al. Feb. 29, 1944 2,374,102 Jahn et al. Apr. 17, 1945 2,717,229 Findlay Sept. 6,1955 2,748,055 Payne May 29, 1956

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2115960 *Apr 2, 1934May 3, 1938Shell DevMethod of treating mineral oils
US2139392 *May 27, 1935Dec 6, 1938Shell DevExtraction process
US2155745 *Jul 1, 1935Apr 25, 1939The Pure Oil ComMethod of preparing lubricating
US2201550 *Jan 15, 1937May 21, 1940Shell DevProcess for the solvent extraction of liquid mixtures
US2228510 *Jun 1, 1939Jan 14, 1941Texas CoConversion of hydrocarbon oils
US2234549 *Jul 17, 1933Mar 11, 1941Union Oil CoProcess for production of lubricating oil
US2270827 *Jul 9, 1940Jan 20, 1942Shell DevProcess for the solvent extraction of liquid mixtures
US2279550 *Mar 31, 1939Apr 14, 1942Universal Oil Prod CoTreatment of cracking stocks
US2304289 *Dec 2, 1939Dec 8, 1942Standard Oil Dev CoConversion of hydrocarbon oils
US2342888 *Dec 31, 1940Feb 29, 1944Standard Oil CoConversion of hydrocarbons
US2374102 *Dec 31, 1940Apr 17, 1945Standard Oil CoConversion of hydrocarbons
US2717229 *Sep 22, 1952Sep 6, 1955Phillips Petroleum CoSolvent extraction process
US2748055 *Jan 4, 1952May 29, 1956Socony Mobil Oil Co IncHydrocarbon conversion process
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3114783 *Aug 27, 1959Dec 17, 1963Exxon Research Engineering CoSeparation of aromatics from hydrocarbon streams
US3206403 *Jul 22, 1964Sep 14, 1965Shell Oil CompanyDistillate and raffinate
US3968023 *Jan 30, 1975Jul 6, 1976Mobil Oil CorporationProduction of lubricating oils
US4311583 *Feb 27, 1980Jan 19, 1982Texaco, Inc.Solvent extraction process
US4981579 *Dec 2, 1988Jan 1, 1991The Standard Oil CompanyProcess for separating extractable organic material from compositions comprising said extractable organic material intermixed with solids and water
US5066386 *Jun 14, 1990Nov 19, 1991The Standard Oil CompanyExtraction of oil from stable oil-water emulsions
US5092983 *Nov 30, 1989Mar 3, 1992The Standard Oil CompanyProcess for separating extractable organic material from compositions comprising said extractable organic material intermixed with solids and water using a solvent mixture
US5186817 *Apr 15, 1991Feb 16, 1993The Standard Oil CompanyProcess for separating extractable organic material from compositions comprising oil-in-water emulsions comprising said extractable organic material and solids
US6146520 *Apr 2, 1997Nov 14, 2000Mobil Oil CorporationSelective re-extraction of lube extracts to reduce mutagenicity index
EP0050381A1 *Sep 25, 1981Apr 28, 1982Shell Internationale Research Maatschappij B.V.Process for the simultaneous separation in aromatics and non-aromatics of a heavy hydrocarbon stream and a light hydrocarbon stream
WO1998044075A1 *Feb 10, 1998Oct 8, 1998Mobil Oil CorpSelective re-extraction of lube extracts to reduce mutagenicity index
U.S. Classification208/312, 208/96, 208/87, 208/18, 208/314
International ClassificationC10G21/00
Cooperative ClassificationC10G21/00
European ClassificationC10G21/00