US2963426A - Color improvement of petroleum lubricating oils - Google Patents
Color improvement of petroleum lubricating oils Download PDFInfo
- Publication number
- US2963426A US2963426A US631994A US63199457A US2963426A US 2963426 A US2963426 A US 2963426A US 631994 A US631994 A US 631994A US 63199457 A US63199457 A US 63199457A US 2963426 A US2963426 A US 2963426A
- Authority
- US
- United States
- Prior art keywords
- oil
- hydrofining
- color
- rerun
- metal hydroxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000010687 lubricating oil Substances 0.000 title claims description 8
- 239000003208 petroleum Substances 0.000 title claims description 8
- 239000003921 oil Substances 0.000 claims description 32
- 239000002585 base Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- 239000003054 catalyst Substances 0.000 claims description 10
- 229910000000 metal hydroxide Inorganic materials 0.000 claims description 10
- 150000004692 metal hydroxides Chemical class 0.000 claims description 9
- 229910052783 alkali metal Inorganic materials 0.000 claims description 5
- 150000001340 alkali metals Chemical class 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 150000004679 hydroxides Chemical class 0.000 claims description 5
- 238000006386 neutralization reaction Methods 0.000 claims description 4
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 3
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 8
- 235000011941 Tilia x europaea Nutrition 0.000 description 8
- 239000004571 lime Substances 0.000 description 8
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 238000007689 inspection Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003518 caustics Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 101150073597 DLST gene Proteins 0.000 description 1
- 101100295675 Dictyostelium discoideum odhB gene Proteins 0.000 description 1
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000004061 bleaching Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- ITRNXVSDJBHYNJ-UHFFFAOYSA-N tungsten disulfide Chemical compound S=[W]=S ITRNXVSDJBHYNJ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/10—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including alkaline treatment as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Definitions
- This invention relates to an improved process for the finishing of petroleum lubricating oil base stocks especially with regard to upgrading and improving their color and stability. More particularly it relates to a process of this nature wherein the unfinished lube oil base stocks are first treated with aqueous alkali metal or alkaline earth hydroxides followed by hydrofining.
- lime is used it is dumped as a powder into a tank containing water and equipped with a paddle to form a water-line slurry representing 10 parts lime and 90 parts water. This slurry is then pumped into the oil line going to the furnace ahead of the pipe still.
- the oil is first contacted with the lime slurry at about 300 F. and passes through the furnace where steam is added and it is heated to a coil outlet temperature of around 700 F. at a pressure of about one atmophere.
- the time of contact in the furnace above'600 F. conveniently isin the range of 30 to 120 sec.
- the thus treated oil is then separated from the spent -metal hydroxide solution by distillation under reduced pressure in a vacuumppipe still.
- the lubricating oil fraction is taken off usually as a sidestream of one or more fractions.
- the alkali or alkaline metal oxide is nonvolatile and is in the small (generally 5% or less) such base stocks prior to hydrofining. By removing aromatic types the stock then becomes sufficiently responsive to hydrofining that the necessary quality improvement can be reached.
- these petroleum lubricating oils can be upgraded, particularly with reference to color improvement, by treating them first with an aqueous metal hydroxide selected from the group consisting of hydroxides of alkali metals and alkaline earth metals, separating the oil from the treating medium by distillation whereby the oil isrerun in contact with the alkaline treating agent and hydrofining the rerun oil in the presence of a hydrofining catalyst.
- an aqueous metal hydroxide selected from the group consisting of hydroxides of alkali metals and alkaline earth metals
- the petroleum lubricating oil base stocks treated are those known in the art. They may be distillates of any width falling within the boiling point range of about 625 to 1150 F. (equivalent atmospheric) or they may be higher boiling fractions recovered by deasphalting from residuum.
- the material to be treated by this process can therefore represent any viscosity in the wide range of 35 up to 180 S.S.U. at 210 F. It applies most particularly to base stocks derived from the naphthenic base crudes such as Tia Juana, Coastal, Lagunillas, etc. It is not restricted to this class of crudes, however, since advantages are also derived by treating base stocks derived from paraffinic base crudes. Examples of particular lube base stocks which can be treated by this process are thus spindle oils, transformer oils, etc.
- the oils are first treated with an aqueous hydroxide as mentioned previously. Because of cost considerations sodium hydroxide or lime (calcium oxide) are preferred. In general, lime is used in an amount of three to four times the theoretical to neutralize the acids confined in the conventional manner.
- Regeneration of the fixed bed catalyst may be required periodically, depending largely upon the nature of the --feed stock. This regeneration is conveniently carried out at a temperature of about 750 to 1000 F. with an oxygen-containing gas.
- the oil and hydrogen are contacted with catalyst by continuous flow through a vessel packed with catalyst.
- the oil feed to the reactor is preheated to the required temperature by means of a furnace or similar means.
- Hydrogen may or may not be heated prior to feeding to the reactor depending on the quantity used.
- the degree of contact of oil saturated with hydrogen with the catalyst is determined by the ratio of the oil flow rate to the catalyst volume.
- the liquid is then passed to a stripper to remove residual H S then it may be fractionated or kept intact.
- a process for upgrading andximproving the color of a petroleum lubricating oil basestock which comprises the steps of treating the oil with a substantial excess of an aqueous metal hydroxide beyond that required 'for neutralization, said metal hydroxide being selectedfrom the group consisting of hydroxides of alkali metals and alkaline earth metals at a temperature within the range of 300 to 700 F.; separating the thus treated oil from the aqueous metal hydroxide by distillation whereby the oil is rerun in direct contact with the alkaline treating agent and hydrofining the rerun oil in the presence of a hydrofining catalyst to produce an oil of improved color and in particular improved heat stability.
- the method of bleaching a spindle oil which comprises treating the said oil with a substantial excess of a hydroxide-beyond that'required for neutralization, said hydroxide 'being selected from the class consisting of the aqueous hydroxides of alkali metals and alkaline earth'metals at temperatures above 600 F., and feed rates ofabout 1 v./v./hr. and the duration of the treatment isfrom 30 to 120 seconds, separating the thus treated oil from the aqueous metal hydroxides by distillation whereby the oil is rerun in direct contact with the alkaline treating agent and hydrofining the oil in the presence of a hydrofining catalyst at temperatures Within therange of 500-700 F. and a pressure within the range of to 1500 p.s.i.g.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
U i ed COLOR IMPROVEMENT F PETROLEUM LUBRICATING ons Clinton H. Holder, Westfield, N.J., assignor to Esso Research and Engineering Company, a corporation of Delaware No Drawing. Filed Jan. 2, 1957, Ser. No. 631,994 Claims. (Cl. 208-286) This invention relates to an improved process for the finishing of petroleum lubricating oil base stocks especially with regard to upgrading and improving their color and stability. More particularly it relates to a process of this nature wherein the unfinished lube oil base stocks are first treated with aqueous alkali metal or alkaline earth hydroxides followed by hydrofining.
The treatment. of petroleum lube base stocks with aqueous caustic or lime is well known at this time for the improvement of the quality thereof. The hydrofining of teS atent 0 M 2,963,426 Patented Dec. 6,1960
tained in the oil. About twice, or less, of the theoretical amount of sodium hydroxide is used. Likewise potassium hydroxide is more reactive than sodium hydroxide. The concentration of the hydroxide in water is not critical and lies in the range of about 10% to 60%. 0 Generally, a 40 Baum strength caustic solution is used.
If lime is used it is dumped as a powder into a tank containing water and equipped with a paddle to form a water-line slurry representing 10 parts lime and 90 parts water. This slurry is then pumped into the oil line going to the furnace ahead of the pipe still. Thus the oil is first contacted with the lime slurry at about 300 F. and passes through the furnace where steam is added and it is heated to a coil outlet temperature of around 700 F. at a pressure of about one atmophere. The time of contact in the furnace above'600 F. conveniently isin the range of 30 to 120 sec.
The thus treated oil is then separated from the spent -metal hydroxide solution by distillation under reduced pressure in a vacuumppipe still. The lubricating oil fraction is taken off usually as a sidestream of one or more fractions. The alkali or alkaline metal oxide is nonvolatile and is in the small (generally 5% or less) such base stocks prior to hydrofining. By removing aromatic types the stock then becomes sufficiently responsive to hydrofining that the necessary quality improvement can be reached.
It has now been found that these petroleum lubricating oils can be upgraded, particularly with reference to color improvement, by treating them first with an aqueous metal hydroxide selected from the group consisting of hydroxides of alkali metals and alkaline earth metals, separating the oil from the treating medium by distillation whereby the oil isrerun in contact with the alkaline treating agent and hydrofining the rerun oil in the presence of a hydrofining catalyst. The results obtained are far superior to those resulting from the individual steps alone or from repeated utilization of each of the individual steps.
The petroleum lubricating oil base stocks treated are those known in the art. They may be distillates of any width falling within the boiling point range of about 625 to 1150 F. (equivalent atmospheric) or they may be higher boiling fractions recovered by deasphalting from residuum.
The material to be treated by this process can therefore represent any viscosity in the wide range of 35 up to 180 S.S.U. at 210 F. It applies most particularly to base stocks derived from the naphthenic base crudes such as Tia Juana, Coastal, Lagunillas, etc. It is not restricted to this class of crudes, however, since advantages are also derived by treating base stocks derived from paraffinic base crudes. Examples of particular lube base stocks which can be treated by this process are thus spindle oils, transformer oils, etc.
The oils are first treated with an aqueous hydroxide as mentioned previously. Because of cost considerations sodium hydroxide or lime (calcium oxide) are preferred. In general, lime is used in an amount of three to four times the theoretical to neutralize the acids confined in the conventional manner.
bottoms fraction. The oil is-thus rerun over the alkaline treating agent preparatory to the hydrofining treatment. The separated oil after this treatment is then hydro- For convenience the conditions are presented below.
Conditions in hydrofiner Broad Range Preferred Range Temperature, F. 500-750 600-725 Pressure, p.s.i.g 100-1. 500 400-800 Feed Rate, v./1r 0. 25-5 0.5-3 Hg Treat. s.c.f./b-. 100-3, 500 500-1. 500 Hg Consumption, s.c.f./b 10-1, 000 -150 'those of the nickel, tungsten sulfide type.
Regeneration of the fixed bed catalyst may be required periodically, depending largely upon the nature of the --feed stock. This regeneration is conveniently carried out at a temperature of about 750 to 1000 F. with an oxygen-containing gas.
In the hydrofining operation, the oil and hydrogen are contacted with catalyst by continuous flow through a vessel packed with catalyst. The oil feed to the reactor is preheated to the required temperature by means of a furnace or similar means. Hydrogen may or may not be heated prior to feeding to the reactor depending on the quantity used. The degree of contact of oil saturated with hydrogen with the catalyst is determined by the ratio of the oil flow rate to the catalyst volume.
After the hydrofining process has been carried out the liquid is then passed to a stripper to remove residual H S then it may be fractionated or kept intact.
The advantages of this invention will be better understood by reference to the following examples.
EXAMPLE A light Tia Juana raw lube distillate having a viscosity of 10 to 105 S.S.U. at F. (column I) was rerun over a lime-water slurry (8 parts lime and 92 parts water) representing four times the theoretical for neutralization of the organic acids. This was done in a batch laboratory distillation employing a vacuum of less than 1 mm. The bottoms yield was 4%. The rerun distillate "had'inspections shownin'column II. A portion of the latter was hydrofined over cobalt molybdate catalyst at 800 p.s.i.g., 800 s.c.f. hydrogen/b., a temperature of 650 F. and a feed rate of 1 v./v./hr. (column.III). A second portion was hydrofin'edlmderfthe' same-conditions except'the temperaturewas 575' F; "(column IV). Another portion ofthe' feed washydrofinedmnder the "same conditions as column 111 but was not given any lime treatment (column V). Inspection datalon these materials were as follows:
-' Hydrofining of Tia Juana lube distillate Q Hydro- Raw Rerun Hydrofined fined Dist. 'Dlst. Rerun Dist. Raw Inspections Dist.
I II III IV V Gravity, API 24. e 24. 2 27. 3 25. 9 27. 2 Visc., SSU:
- 102. 5 87.3 94.4 87.2 v 38. 2 37. 3 37. 7 37. 1 Vise. Index-. I 25. 8 48. 1 84.2 48 Neut. N0. mgs. KOH/g 1.6 0.18 .05 .06 .08 Color, T.R 6 9% 18% 18% 13 Colorhold, T.R. 4 8%; 17% 14 11% Pour Point, F 45 -45 35 -40 -40 Color stability test-actual color after 16 hours at 212 F.
These' data demonstrate that the: lime treatrnent alone gave a product of only 9 /2 Tag Robinson whereas hydrofining alone gave a Tag Robinson number of 13. Only the combination of thetwo steps :of this invention, columns III and IV, gave a Tag number of at least 18 or enough to satisfy specifications. Furthermore, the material produced at 650 F. and 1 v./v./hr. was shown to exhibit good color stability.
In other work it has been shown that spindle oils of this color can be made if the raw lube distillate is first extracted to a yield of about 80% before hydrofining. This is less desirable than the present process because the yields are reduced, extraction is more expensive than rerunning and solvent contamination in. the extraction plant becomes a problem when such light-stocks as this are extracted.
The advantages of this inventionWill-be apparent to the skilled in the art. It can be used in either of two ways. Either, improved products of superior'color characteristics are obtained in a simple, economical process, or, the use of the treatment with metal hydroxide before it This in turn yields products with less increase in pour point.
It is to be understood that this invention is not limited to the specific examples which have been offered merely as illustrations and that modifications may be made without departing from the spirit of the invention.
What is claimed is:
1. A process for upgrading andximproving the color of a petroleum lubricating oil basestock which comprises the steps of treating the oil with a substantial excess of an aqueous metal hydroxide beyond that required 'for neutralization, said metal hydroxide being selectedfrom the group consisting of hydroxides of alkali metals and alkaline earth metals at a temperature within the range of 300 to 700 F.; separating the thus treated oil from the aqueous metal hydroxide by distillation whereby the oil is rerun in direct contact with the alkaline treating agent and hydrofining the rerun oil in the presence of a hydrofining catalyst to produce an oil of improved color and in particular improved heat stability.
2. The process of claim 1 in which the metal hydrox- "ide treating step is conducted above 600 F. for to 'to 750"F. and a pressure in the range of 100 to 1500 hydrofining permits of mildcrconditions for the latter.
4."The process ofclaim' 3 is' in which the base stock has a viscosity of 35 to 180 S.S.U. at 210 F.
5. The method of bleaching a spindle oil which comprises treating the said oil with a substantial excess of a hydroxide-beyond that'required for neutralization, said hydroxide 'being selected from the class consisting of the aqueous hydroxides of alkali metals and alkaline earth'metals at temperatures above 600 F., and feed rates ofabout 1 v./v./hr. and the duration of the treatment isfrom 30 to 120 seconds, separating the thus treated oil from the aqueous metal hydroxides by distillation whereby the oil is rerun in direct contact with the alkaline treating agent and hydrofining the oil in the presence of a hydrofining catalyst at temperatures Within therange of 500-700 F. and a pressure within the range of to 1500 p.s.i.g.
' References Cited in the file of this patent UNITED STATES PATENTS 1,998,765 Logan -..Apr; 23, 1935 2,451,025 Ellender Oct. 12, 1948 2,654,696 La Porte Oct. 6, 1953 1,773,807 Blatz -*Dec. 11, 1956
Claims (1)
1. A PROCESS FOR UPGRADING AND IMPROVING THE COLOR OF A PETROLEUM LUBRICATING OIL BASE STOCK WHICH COMPRISES THE STEPS OF TREATING THE OIL WITH A SUBSTANTIAL EXCESS OF AN AQUEOUS METAL HYDROXIDE BEYOND THAT REQUIRED FOR NEUTRALIZATION, SAID METAL HYDROXIDE BEING SELECTED FROM THE GROUP CONSISTING OF HYDROXIDES OF ALKALI METALS AND ALKALINE EARTH METALS AT A TEMPERATURE WITHIN THE RANGE OF 300* TO 700*F., SEPARATING THE THUS TREATED OIL FROM THE AQUEOUS METAL HYDROXIDE BY DISTALLATION WHEREBY THE OIL IS RERUN IN DIRECT CONTACT WITH THE ALKALINE TREATING AGENT AND HYDROFINING THE RERUN OIL IN THE PRESENCE OF A HYDROFINING CATALYST TO PRODUCE AN OIL OF IMPROVED COLOR AND IN PARTICULAR IMPROVED HEAT STABILITY.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US631994A US2963426A (en) | 1957-01-02 | 1957-01-02 | Color improvement of petroleum lubricating oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US631994A US2963426A (en) | 1957-01-02 | 1957-01-02 | Color improvement of petroleum lubricating oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2963426A true US2963426A (en) | 1960-12-06 |
Family
ID=24533642
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US631994A Expired - Lifetime US2963426A (en) | 1957-01-02 | 1957-01-02 | Color improvement of petroleum lubricating oils |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2963426A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3192153A (en) * | 1962-11-06 | 1965-06-29 | Socony Mobil Oil Co Inc | Preparation of transformer oils |
| US3378485A (en) * | 1965-08-23 | 1968-04-16 | Getty Oil Co | Clarification of caustic treated distillate fuels |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1998765A (en) * | 1931-10-08 | 1935-04-23 | Texas Co | Process for neutralizing organic acidity in petroleum lubricating oils |
| US2451025A (en) * | 1945-11-15 | 1948-10-12 | Standard Oil Dev Co | Method of refining lubricating oils |
| US2654696A (en) * | 1950-06-02 | 1953-10-06 | Sun Oil Co | Treatment of lubricating oil |
| US2773807A (en) * | 1956-12-11 | Repmevg nakfflotnic lube-oil distoxatos |
-
1957
- 1957-01-02 US US631994A patent/US2963426A/en not_active Expired - Lifetime
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2773807A (en) * | 1956-12-11 | Repmevg nakfflotnic lube-oil distoxatos | ||
| US1998765A (en) * | 1931-10-08 | 1935-04-23 | Texas Co | Process for neutralizing organic acidity in petroleum lubricating oils |
| US2451025A (en) * | 1945-11-15 | 1948-10-12 | Standard Oil Dev Co | Method of refining lubricating oils |
| US2654696A (en) * | 1950-06-02 | 1953-10-06 | Sun Oil Co | Treatment of lubricating oil |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3192153A (en) * | 1962-11-06 | 1965-06-29 | Socony Mobil Oil Co Inc | Preparation of transformer oils |
| US3378485A (en) * | 1965-08-23 | 1968-04-16 | Getty Oil Co | Clarification of caustic treated distillate fuels |
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