US2081473A - Process for treating oils - Google Patents

Process for treating oils Download PDF

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US2081473A
US2081473A US709836A US70983634A US2081473A US 2081473 A US2081473 A US 2081473A US 709836 A US709836 A US 709836A US 70983634 A US70983634 A US 70983634A US 2081473 A US2081473 A US 2081473A
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oil
propane
line
passes
asphalt
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US709836A
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Ulric B Bray
Claude E Swift
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Union Oil Company of California
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Union Oil Company of California
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Priority to US555017A priority Critical patent/US1988712A/en
Priority to FR740803D priority patent/FR740803A/en
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    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/02—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils
    • C10G73/06—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils with the use of solvents
    • 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
    • C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
    • C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
    • C10G17/04—Liquid-liquid treatment forming two immiscible phases
    • C10G17/06—Liquid-liquid treatment forming two immiscible phases using acids derived from sulfur or acid sludge thereof
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting

Definitions

  • This invention relates toV a process for treating petroleum to produce lubricating oil and is a division of our copending application Serial No. 555,017, filed August 4th, 1931. More particularly, the invention relates to the separation of asphalt from oil.
  • a further object of our invention is to separate the asphalt from gil by means of liqueed normally gaseous hydrocarbon solvents, such as liquid propane, at temperatures above ordinary room or normal temperaturesand under superatmospheric pressure.
  • Another object of our invention is to separate wax from oils containing the same subsequent to de-asphaltizing the oil at elevated temperatures.
  • a further object olf our invention is to treat the oil with chemicals, such as sulphuric acid and clay, in the presence of a solvent subsequent to deasphaltizing at elevated temperatures and also to separate the oil into parafnoid and non-paraflinoid fractions by means of a selective solvent, such' as liquid sulphur dioxide.
  • chemicals such as sulphuric acid and clay
  • a solvent is chosen which is capable of dissolving the oil and wax but which does not dissolve the asphalt.
  • solvents we may employ light petroleum fractions,'such as naphtha, casinghead gasoline and petroleum fractions normally vaporousl vat ordinary temperature and ⁇ pressure'.
  • Other solvents which may be used are (ICI. ISS-13) alcohol, ether, mixtures of alcohol and ether,
  • a liquefied normally gaseous hydrocarbon such as a petroleum fraction obtained by the rectiiication of natural gasoline.
  • solvents comprise methane, ethane, propane, butano or mixtures thereof.
  • a typical analysis of such a fraction ⁇ is 6.72% ethane, '72.2% propane, 19.91% isobutane and ⁇ 1.17% normal butane.
  • This fraction is liquid at ordinary temperatures at a pressure of about lbs. per square inch.
  • the vaporized ,propane in line 'I is compressed by compressor 8 and sent to condenser 9 where it is liqueed and passes by means of line I0 to pro-4 pane storage tank I I.
  • the cooled mass of topped crude and liquid propane in chiller 5' passes by means of line I5 to agitator I6 Where it is thoroughly mixed, after which it passes by means of line I1 to decanter I8 Where the asphalt settles out.
  • the asphalt in decanter I8 is removed through Valve I9 and sent by pump 20 through line 2
  • the heatedv mass then passes by means of line 23 into separator 24 l where the asphalt separates out and is removed through valve 25 and line 26 to storage tank 21.
  • the mixture of Water vapor and propane passes from separator 24 through line 28 to condenser 29 where the water vapor is condensed.
  • the mixture of Water and propane vapor passes from condenser 29 to separator 30 where the Water is separated' out and is removed through valve 3l and line 32.
  • the propane vapor in separator 30 passes by means of line 33 to cornpressor 34 Where it is compressed and sent by means of lines 33 and,'l2 to condenser 9 where it is liquefied and' passes through lline I0 to Vstorage tank II.
  • the propane solution of oil in decanter I8 is withdrawn through line 35 and passes into chiller -36 where the temperature of the mass is lowered to a point sumcient to cause thorough'wax preo cipitation by allowing a portion of the propane present in chiller 36 to vaporize under reduced pressure through valve 31 into line 38.
  • the propane vapor in line 38 is compressed by compressor 39 and.sent through lines 38 and 12' 55 sulphur dioxide present.
  • stage 43 into line 44 whereit is mixed with sulphuric acid coming from tank 45 through valve 46, line 41, pump 48 and line 41'.
  • the mixture of oil and acid then passes into agitator 49 where it is thoroughly mixed, after which it passes into decanter 5
  • is removed through valve 53 and sent by means of pump 54 through line 55 to heater 56 where the temperature of the mass is raised sufficiently to vaporize the propane.
  • the heated mass then passes by means of line 51 to separator 58 where the sludge separates out and is withdrawn through valve 59 and line 00.
  • the propane vapor passes from separator 58 through line 6
  • the scrubbed propane passes from tower 62 throughvalve 88, line 61, compressor 88, lines 81' and 12' to condenser 9 where it is liqueed and passes by means of line I0 to storagel tank
  • passes by means lof line 52 to clay tower
  • the propane solution of treated oil then passes from tower
  • the propane vapor passes from evaporator 10 through valve 1
  • 'I'he propane free oil in evaporator 10 is withdrawn through valve 15 and passes through cooler 10 where the temperature is lowered suiiiciently for extraction with a selective solvent such as liquid sulphur dioxide which is adapted to separate the oil into parafnoid and non-paraiinoid fractions.
  • a selective solvent such as liquid sulphur dioxide which is adapted to separate the oil into parafnoid and non-paraiinoid fractions.
  • the cooled oil passes from cooler 16 y to pump 11 which forces it through line 18 into ing the non-paramnoid fractions which are removed in the form of a sulphur-dioxide solution through valve 94 into line 95 from Which the mixture passes into evaporator 96 where the sulphur dioxide present is removed with the aid of steam introduced into closed steam coil
  • the sulphur dioxide free ou 1n evaporator 9s is withdrawn through valve 98 and passes by means of line 9 9 to storage tank
  • liquid sulphur dioxide as a selective solvent for separating the oil into paraf- ⁇ iinoid and non-parafnoid oils
  • solventagents which will eiect this separation, mixtures of acetone and benzol, aniline or methyl formate.
  • liquid sulphur dioxide has of liquid sulphur dioxide, it is possible to separate
  • oils which have a low temperature viscosity susceptibility oils which have a high temperature viscosity susceptibility.
  • the topped oiLin tank l at a temperature approximating 200 F., is mixed with liquid propane and cooled by allowing a portion of the propane present to vaporize until an elevated temperature of about F. is attained, after which the mixture of residual oil and propane is mixed in agitator i6.
  • the thoroughly agitated mass passes into decanter I8 where the propane solution of oiland wax is separated from the undissolved asphalt.
  • This oil dissolved in liquid propane which is a mixture oi paraiiinoid and non-paraflinoid oils, is chilled sufficiently to cause the wax present to precipitate out by allowing a further portion of the propane present to vaporize under reduced pressure.
  • the precipitated .wax ⁇ is removed from the solvent solution of oil by such means as cold settling, centrifuging or lter pressing; 'I'he oil substantially free of wax and asphalt dissolved in solvent is next treated with sulphuric acid introduced from tank 45.
  • 'I'he result of this -treatment is to remove further quantities -of undesirable bodies present in the oil which tend to give the finished product an increased viscosity temperature susceptibility.
  • the oil is separated from 'the solvent and then extracted with liquid sulphur dioxide for the purpose of separating the parafiinoid from the non-paraflinoid constituents.
  • the oil may be extracted with liquid sulphur dioxide immediately following the de- 'asphaltizing and dewaxing stages and subsequent to theL separation of propane from the asphalt and wax free oil after which the paramnoid fractions may be commingled with liquid propane and the mixture treated with acid andclay.
  • This procedure has been described in our 4copending application No. 555,017.
  • the oil may be chemically treated in the presence of the propane subsequent to deasphaltizing after which the propane is Vseparated and the oil extracted with liquid sulphur dioxide, or the deasphaltized oil may be extracted with liquid sulphur dioxide and the parafflnoid fraction chemically treated. ⁇ These procedures have been described in our copendng application Serial No. 555,016.
  • the extraction of the deasphaltized oil with liquid sulphur dioxide may be accom- ⁇ plished in the presence of liquid propane as described in our copending application Ser. No. 555,018.
  • the temperature of the deasphaltized oil-propane mixture is further re ⁇ pokerd to an extraction temperature by vaporizing propane under reduced pressure.
  • the paraffinoid fraction may then be dewaxed in the presence of liquid propane and then chemically treated also in the presence of liquid propane.
  • a process for separ'ating asphalt from oils containing the same which comprises commingling said oil at an elevated temperature of at 4,0 least 120 F. with aliquefied normally gaseous hydrocarbon solvent and separating said asphalt from said oil and solvent at an elevated temperature.
  • a process for separating asphalt from oils containing the same which comprises mixing said oil under superatmospheric pressure at an elenormally gaseous hydrocarbon solvent in which oil is soluble and in which asphalt is insoluble and separating said asphalt from said oil and solvent. under superatmospheric pressure at an elevated perature of the mixture to an elevated temperature of approximately 120 F.' and separating asphalt from oil and solvent at said last mentioned elevated temperature.
  • a process as in claim 5 in which the temperature of the mixture is reduced to approximately 120 F. by vaporizing a portion of the solvent under reduced pressure.
  • a 'process for separating asphalt from oils containing the same which comprises heating said oil to an elevated temperature of at 1east 120 F., mixing said heated oil While at said temperature with a liquefied normally gaseous hydrocarbon to precipitate asphalt and separating the precipitated asphalt from the oil and liquefied normally gaseous hydrocarbon.

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  • 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

May 25, 193?. u. B. BRAY r AL PROCESS FOR TREATING OILS Original Filed Aug. 4, 1931 atented` ay 25, i937 PROCESS FOR TREATING OILS Original application August 4, 1931, Serial No.
555,019. Divided and this application February 5, 1934, Serial No. 709,836
9 claims.
This invention relates toV a process for treating petroleum to produce lubricating oil and is a division of our copending application Serial No. 555,017, filed August 4th, 1931. More particularly, the invention relates to the separation of asphalt from oil.
It is an object of our invention to separate asphalt from oil by means of a solvent at an elevated temperature. A further object of our invention is to separate the asphalt from gil by means of liqueed normally gaseous hydrocarbon solvents, such as liquid propane, at temperatures above ordinary room or normal temperaturesand under superatmospheric pressure.
Itis another object of our invention to separate the asphalt from oils at temperatures above 75 F. and more particularly at temperatures of approximately 120 F.
Another object of our invention is to separate wax from oils containing the same subsequent to de-asphaltizing the oil at elevated temperatures. To separate the wax, We prefer to vaporize a portion of the solvent under reduced pressure. This will chill the oil and cause the Wax to precipitate from solution.
A further object olf our invention is to treat the oil with chemicals, such as sulphuric acid and clay, in the presence of a solvent subsequent to deasphaltizing at elevated temperatures and also to separate the oil into parafnoid and non-paraflinoid fractions by means of a selective solvent, such' as liquid sulphur dioxide.
Itis another object to effect the separation or extraction of the oil subsequent to deasphaltizing either in the presence or substantial absence of a diluent as liquid propane.
Other objects and features of our invention will be understood by referring to the drawing which represents a schematic arrangement of one form of apparatus in which our process may be carried out.
Referring more particularly to the drawing,
crude oil from which all of the gasoline, kerosene and gas oil has been removed in tank I is with- 4 drawn through valve 2 and sent by means of pump I un 3 to line 4 where it meets a stream of solvent corn-4 ing from storage tank II through valve `I2 pump I3 and line I4. A solvent is chosen which is capable of dissolving the oil and wax but which does not dissolve the asphalt. As solvents, ,we may employ light petroleum fractions,'such as naphtha, casinghead gasoline and petroleum fractions normally vaporousl vat ordinary temperature and` pressure'. Other solvents which may be used are (ICI. ISS-13) alcohol, ether, mixtures of alcohol and ether,
acetone, etc. We prefer to use as our solvent a liquefied normally gaseous hydrocarbon such as a petroleum fraction obtained by the rectiiication of natural gasoline. Such solvents comprise methane, ethane, propane, butano or mixtures thereof. A typical analysis of such a fraction` is 6.72% ethane, '72.2% propane, 19.91% isobutane and `1.17% normal butane. This fraction is liquid at ordinary temperatures at a pressure of about lbs. per square inch.
The mixture of topped crude and liqueed normally gaseous hydrocarbon solvent, such as liquid propane under pressure, passes into chiller 5 where the mass is cooled by allowing a portion of the liquid propane to vaporize under reduced pressure through valve 6 intoy line l. The vaporized ,propane in line 'I is compressed by compressor 8 and sent to condenser 9 where it is liqueed and passes by means of line I0 to pro-4 pane storage tank I I. The cooled mass of topped crude and liquid propane in chiller 5' passes by means of line I5 to agitator I6 Where it is thoroughly mixed, after which it passes by means of line I1 to decanter I8 Where the asphalt settles out.
The asphalt in decanter I8 is removed through Valve I9 and sent by pump 20 through line 2| to heater 22 where the temperature ofthe mass is raised suiiciently to vaporize all of the propane '30 and moisture present. The heatedv mass then passes by means of line 23 into separator 24 l where the asphalt separates out and is removed through valve 25 and line 26 to storage tank 21. The mixture of Water vapor and propane passes from separator 24 through line 28 to condenser 29 where the water vapor is condensed. The mixture of Water and propane vapor passes from condenser 29 to separator 30 where the Water is separated' out and is removed through valve 3l and line 32. The propane vapor in separator 30 passes by means of line 33 to cornpressor 34 Where it is compressed and sent by means of lines 33 and,'l2 to condenser 9 where it is liquefied and' passes through lline I0 to Vstorage tank II.
The propane solution of oil in decanter I8 is withdrawn through line 35 and passes into chiller -36 where the temperature of the mass is lowered to a point sumcient to cause thorough'wax preo cipitation by allowing a portion of the propane present in chiller 36 to vaporize under reduced pressure through valve 31 into line 38. The propane vapor in line 38 is compressed by compressor 39 and.sent through lines 38 and 12' 55 sulphur dioxide present.
stage 43 into line 44 whereit is mixed with sulphuric acid coming from tank 45 through valve 46, line 41, pump 48 and line 41'. The mixture of oil and acid then passes into agitator 49 where it is thoroughly mixed, after which it passes into decanter 5| where the` sludge is allowed to settle out. rThe sludge in decanter 5| is removed through valve 53 and sent by means of pump 54 through line 55 to heater 56 where the temperature of the mass is raised sufficiently to vaporize the propane. The heated mass then passes by means of line 51 to separator 58 where the sludge separates out and is withdrawn through valve 59 and line 00. The propane vapor passes from separator 58 through line 6| to scrubbing tower 62 where it is contacted with liquid caustic soda to remove any The scrubbed propane passes from tower 62 throughvalve 88, line 61, compressor 88, lines 81' and 12' to condenser 9 where it is liqueed and passes by means of line I0 to storagel tank The acid treated oil dissolved in propane in decanter 5| passes by means lof line 52 to clay tower |25 where any remaining sludge iseremoved. The propane solution of treated oil then passes from tower |25 by meansolline 69 to evaporator 10 where the propane present is vaporized with the aid of steam introduced through closed steam coil 14. The propane vapor passes from evaporator 10 through valve 1| into line 12 thence to compressor 13 where it is compressed and sent by means of line 12' lto condenser 9y where it is liquefied Vand passes by means of line |20 to storage tank il.
'I'he propane free oil in evaporator 10 is withdrawn through valve 15 and passes through cooler 10 where the temperature is lowered suiiiciently for extraction with a selective solvent such as liquid sulphur dioxide which is adapted to separate the oil into parafnoid and non-paraiinoid fractions. The cooled oil passes from cooler 16 y to pump 11 which forces it through line 18 into ing the non-paramnoid fractions which are removed in the form of a sulphur-dioxide solution through valve 94 into line 95 from Which the mixture passes into evaporator 96 where the sulphur dioxide present is removed with the aid of steam introduced into closed steam coil |05 passes through valve 91 into line 90 and thence to compressor |0l where it is compressed and passes by means of line ,90' to condenser |02 where it is liqueiied and passes by means of line |03 to sulphur dioxide storage 19. The sulphur dioxide free ou 1n evaporator 9s is withdrawn through valve 98 and passes by means of line 9 9 to storage tank |00.
'I'he ascending column of oil in column |04 from which there has been removed the sulphur dioxide soluble constituents, passes through valve'83 and line 84 into auxiliary settling chamber 85 where any remaining liquid sulphur dioxide settles out. The settled oil from chamber 85 passes through line 81 into4 evaporator 88 where the sulphur dioxide present is vaporized by aid of steam introduced into closed steam coil |06 and passes through Valve 89 to line 90 and thence to compressor |0| where it is liqueiied and passes by means of line |03 to sulphur dioxide storage tank 19. The sulphur dioxide free oil in evaporator 88 is withdrawn through valve 9| and-sent by means ofiine 92 to refined oil storage tank 93.
Instead of employing liquid sulphur dioxide asa selective solvent for separating the oil into paraf- `iinoid and non-parafnoid oils, we may employ as solventagents which will eiect this separation, mixtures of acetone and benzol, aniline or methyl formate. However, liquid sulphur dioxide has of liquid sulphur dioxide, it is possible to separate,
this material into oils which have a low temperature viscosity susceptibility and oils which have a high temperature viscosity susceptibility.
As illustrative of the operation of the process for one .type of oil without intending to limit our invention, the following is an example:
The topped oiLin tank l, at a temperature approximating 200 F., is mixed with liquid propane and cooled by allowing a portion of the propane present to vaporize until an elevated temperature of about F. is attained, after which the mixture of residual oil and propane is mixed in agitator i6. The thoroughly agitated mass passes into decanter I8 where the propane solution of oiland wax is separated from the undissolved asphalt. This oil dissolved in liquid propane, which is a mixture oi paraiiinoid and non-paraflinoid oils, is chilled suficiently to cause the wax present to precipitate out by allowing a further portion of the propane present to vaporize under reduced pressure. The precipitated .wax `is removed from the solvent solution of oil by such means as cold settling, centrifuging or lter pressing; 'I'he oil substantially free of wax and asphalt dissolved in solvent is next treated with sulphuric acid introduced from tank 45. 'I'he result of this -treatment is to remove further quantities -of undesirable bodies present in the oil which tend to give the finished product an increased viscosity temperature susceptibility. After treatment:with sulphuric acid, the oil is separated from 'the solvent and then extracted with liquid sulphur dioxide for the purpose of separating the parafiinoid from the non-paraflinoid constituents.
Ii desired, the oil may be extracted with liquid sulphur dioxide immediately following the de- 'asphaltizing and dewaxing stages and subsequent to theL separation of propane from the asphalt and wax free oil after which the paramnoid fractions may be commingled with liquid propane and the mixture treated with acid andclay. This procedure has been described in our 4copending application No. 555,017. By performing the acid treatment step in the-process subsequent to treatment with liquid sulphur dioxide more economical and eective results are obtained in that the acid utilized in such treatment is free to act upon those-undesirable bodies present in the oil which are not removable by liquid sulphur dioxide. By acid treating theI Qil prior to extraction with liquid sulphur dioxide, a large portion of the acid is consumed in removing from the oil unsaturated bodies which are easily removable with liquid sulphur dioxide.
If desired, the oil may be chemically treated in the presence of the propane subsequent to deasphaltizing after which the propane is Vseparated and the oil extracted with liquid sulphur dioxide, or the deasphaltized oil may be extracted with liquid sulphur dioxide and the parafflnoid fraction chemically treated. `These procedures have been described in our copendng application Serial No. 555,016.
If desired, the extraction of the deasphaltized oil with liquid sulphur dioxide may be accom-` plished in the presence of liquid propane as described in our copending application Ser. No. 555,018. In such case the temperature of the deasphaltized oil-propane mixture is further re` duced to an extraction temperature by vaporizing propane under reduced pressure. The paraffinoid fraction may then be dewaxed in the presence of liquid propane and then chemically treated also in the presence of liquid propane.
The foregoing description is merely illustrative of preferred modes of carrying out our in- `vention and is not to be taken as limiting as many variations may be made within the scope of the following claims by persons skilled in the art without departing from the spirit thereof.
`We claim:
1. A process for separ'ating asphalt from oils containing the same which comprises commingling said oil at an elevated temperature of at 4,0 least 120 F. with aliquefied normally gaseous hydrocarbon solvent and separating said asphalt from said oil and solvent at an elevated temperature.
2. A process for separating asphalt from oils containing the same which comprises mixing said oil under superatmospheric pressure at an elenormally gaseous hydrocarbon solvent in which oil is soluble and in which asphalt is insoluble and separating said asphalt from said oil and solvent. under superatmospheric pressure at an elevated perature of the mixture to an elevated temperature of approximately 120 F.' and separating asphalt from oil and solvent at said last mentioned elevated temperature.
6. A process as in claim 5 in which the temperature of the mixture is reduced to approximately 120 F. by vaporizing a portion of the solvent under reduced pressure.
rI. A process as in claim 1 in which the liqueed normally gaseous hydrocarbon solvent comprises propane.
8. A 'process for separating asphalt from oils containing the same which comprises heating said oil to an elevated temperature of at 1east 120 F., mixing said heated oil While at said temperature with a liquefied normally gaseous hydrocarbon to precipitate asphalt and separating the precipitated asphalt from the oil and liquefied normally gaseous hydrocarbon.
9. A process as in claim 8 in which the liquefied normally gaseous hydrocarbon solvent com prises propane.
ULRIC B. BRAY. CLAUDE E. SWIFT.
vvated temperature of at least 120 F. in a liqueed
US709836A 1931-08-04 1934-02-05 Process for treating oils Expired - Lifetime US2081473A (en)

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US555017A US1988712A (en) 1931-08-04 1931-08-04 Process for production of lubricating oil
FR740803D FR740803A (en) 1931-08-04 1932-07-20 Process improvements for the production of lubricating oil
US709836A US2081473A (en) 1931-08-04 1934-02-05 Process for treating oils

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US555017A US1988712A (en) 1931-08-04 1931-08-04 Process for production of lubricating oil
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3095368A (en) * 1957-07-31 1963-06-25 Exxon Research Engineering Co Process for removing metallic contaminants from oils
US4358365A (en) * 1981-04-24 1982-11-09 Uop Inc. Conversion of asphaltene-containing charge stocks
US4364819A (en) * 1981-04-24 1982-12-21 Uop Inc. Conversion of asphaltene-containing charge stocks
US6447671B1 (en) 1999-03-25 2002-09-10 Institut Francais Du Petrole Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step
US10494579B2 (en) 2016-04-26 2019-12-03 Exxonmobil Research And Engineering Company Naphthene-containing distillate stream compositions and uses thereof
US10550341B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Sequential deasphalting for base stock production
US10550335B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Fluxed deasphalter rock fuel oil blend component oils
US10590360B2 (en) 2015-12-28 2020-03-17 Exxonmobil Research And Engineering Company Bright stock production from deasphalted oil

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE747401C (en) * 1937-06-26 1945-01-18 Steinkohlen Bergwerk Rheinpreu Process for the processing of coal tar oil in the settlement area 180 to 350íÒ
US2429430A (en) * 1944-12-02 1947-10-21 Schutte August Henry Wax-oil separation
US2546916A (en) * 1948-10-19 1951-03-27 Socony Vacuum Oil Co Inc Method of refining hydrocarbon lubricating oils
US2764529A (en) * 1951-08-18 1956-09-25 Exxon Standard Sa Steam cylinder lubricating oil

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3095368A (en) * 1957-07-31 1963-06-25 Exxon Research Engineering Co Process for removing metallic contaminants from oils
US4358365A (en) * 1981-04-24 1982-11-09 Uop Inc. Conversion of asphaltene-containing charge stocks
US4364819A (en) * 1981-04-24 1982-12-21 Uop Inc. Conversion of asphaltene-containing charge stocks
US6447671B1 (en) 1999-03-25 2002-09-10 Institut Francais Du Petrole Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step
US10550341B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Sequential deasphalting for base stock production
US10550335B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Fluxed deasphalter rock fuel oil blend component oils
US10590360B2 (en) 2015-12-28 2020-03-17 Exxonmobil Research And Engineering Company Bright stock production from deasphalted oil
US10647925B2 (en) 2015-12-28 2020-05-12 Exxonmobil Research And Engineering Company Fuel components from hydroprocessed deasphalted oils
US10808185B2 (en) 2015-12-28 2020-10-20 Exxonmobil Research And Engineering Company Bright stock production from low severity resid deasphalting
US10947464B2 (en) 2015-12-28 2021-03-16 Exxonmobil Research And Engineering Company Integrated resid deasphalting and gasification
US10494579B2 (en) 2016-04-26 2019-12-03 Exxonmobil Research And Engineering Company Naphthene-containing distillate stream compositions and uses thereof

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FR740803A (en) 1933-02-01
US1988712A (en) 1935-01-22

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