US3773650A - Dewaxing process - Google Patents

Dewaxing process Download PDF

Info

Publication number
US3773650A
US3773650A US00129973A US3773650DA US3773650A US 3773650 A US3773650 A US 3773650A US 00129973 A US00129973 A US 00129973A US 3773650D A US3773650D A US 3773650DA US 3773650 A US3773650 A US 3773650A
Authority
US
United States
Prior art keywords
mixture
solvent
oil
stages
wax
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
Application number
US00129973A
Other languages
English (en)
Inventor
D Hislop
J Eagen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Exxon Mobil Corp
Original Assignee
Exxon Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Exxon Corp filed Critical Exxon Corp
Application granted granted Critical
Publication of US3773650A publication Critical patent/US3773650A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • 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
    • C10G73/32—Methods of cooling during dewaxing
    • 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

Definitions

  • ABSTRACT An improved process for the solvent dewaxing of pe- 1 troleum oil stocks.
  • the dewaxing solvent is prechilled and added incrementally or continuously at several points along the height of a cooling tower.
  • the oilsolvent mixture is agitated during the chilling step to permit substantially instantaneous mixing of the prechilled solvent with the oil.
  • This invention relates to a process for dewaxing petroleum oil stocks. More particularly, this invention relates to a process wherein selective dewaxing solvents are used to facilitate the precipitation of wax from waxy petroleum oil stocks. Still more particularly, this invention relates to a process wherein the wax is pre- .cipitated by incremental or continuous addition of a prechilled selective solvent along the height of a vertical, stirred chilling tower.
  • the temperature of the incrementally added solvent should be the same as that of the main stream at the point of addition. Having the solvent at a lower temperature causes shock chilling of the slurry at that point, with resulting formation of crystal fines, and impairment of filter rate; having the solvent warmer throws an unnecessary additional load on the scraped surface chillers.
  • waxy petroleum stocks are dewaxed bycooling the petroleum oil stock in an elongated stirred vessel, preferably a vertical tower, with a prechilled solvent that will solubilize at least a portion of the oil stock.
  • the solvent is preferably introduced incrementally along the length of the vessel. It is necessary that the degree of agitation in the stirred, elongated vessel be sufficient to permit substantially instantaneous mixing of the oil and solvent.
  • the prechilled solvent is added in an amount sufficient to permit easy handling and good filtration rates.
  • the wax, which precipitates during the cooling stage may be separated from the solution by conventional means known in the art. Following separation of the wax, the oil, which has a reduced pour and cloud point, is recovered from the solution by means well known in the art.
  • FIGURE is a flow diagram of the dewaxing process of the invention.
  • DETAILED DESCRIPTION solvent for the oil stock is passed from storage tank 5 through line 6, through heat exchangers 7 and 8, where the solvent temperature is reduced to a level sufficient to cool the oil to the desired dewaxing temperature.
  • Coolant enters the heat exchangers 7 and 8 through lines 24 and 25, respectively, and leaves through lines 26 and 27.
  • the solvent leaves the heat exchanger 8, through line 9, and enters manifold 10.
  • the manifold comprises a series of parallel lines providing solvent inlets 11 to the several stagesof the cooling tower 3.
  • the rate of flow through each inlet is regulated by flow control means (not shown),
  • the rate of solvent flow is regulated so as to maintain a desired temperature gradient along the height of the cooling tower 3.
  • the first portion or ihcrement of the solvent enters the first stage, 4(a), of the cooling tower 3 where it is substantially instantaneously admixed with oil due to theaction of the agitator 12(a).
  • the agitator is driven by a variable speed motor 13 and the degree of agitation is controlled by variation of the motor speed, with due allowance for the flow rate through the cooling tower.
  • the oil-solvent mixture may pass upwardly or downwardly through the cooling tower 3 (downward flow only has been shown).
  • Additional prechilled solvent is introduced into at least a portion of the several stages 4, through inlets 11 so as to maintain a substantially constant cooling rate and at the same time to provide the desired degree of dilution. It should be noted that any number of stages, for example fifty may be employed; however, it is desirable that at least six stages be used.
  • the oil-solvent solution with precipitated wax passes from the final stage of the cooling tower through line 14 to means for separating the wax from said solution 15. Any suitable means, such as filtration or centrifugation, for such separation may be employed.
  • the waxsolvent is removed from the separation means through line 16.
  • the solvent is recovered in a suitable separating system 19, which is preferably a distillation tower,
  • oil-solvent solution leaves the wax separation means through line 20 and passes to means for separating the oil from solution 21. Any suitable means for this separation may be used, such as distillation or selective adsorption.
  • the oil is removed from the separator and is recovered through line 22.
  • the solvent is removed through line 23.
  • waxy petroleum oil stock or distillate fraction thereof may be dewaxed with the process of this invention.
  • these oil stocks or distillate fractions will have a boiling range within the broad range of about 500F. to about 1300F.
  • the preferred oil stocks are the lubricating oil and specialty oil fractions boiling within the range of 550F. and 1200F.
  • These fractions may come from any source, such as the paraffinic crudes obtained from Aramco, Kuwait, the Panhandle, North Louisiana, Tia Juana, etc.
  • any selective solvent may be used in the process of this invention.
  • solvents are (a) the aliphatic ketones having from 3 to 6 carbon atoms, such as acetone, methyl ethyl ketone (MEK), and methyl isobutyl ketone (MIBK), and (b) the low molecular weight hydrocarbons such as ethane, propane, butane, and propylene, as well as mixtures of the foregoing ketones and mixtures of the aforesaid ketones with aromatic compounds such as benzene and toluene.
  • the aliphatic ketones having from 3 to 6 carbon atoms such as acetone, methyl ethyl ketone (MEK), and methyl isobutyl ketone (MIBK)
  • the low molecular weight hydrocarbons such as ethane, propane, butane, and propylene
  • halogenated low molecular weight hydrocarbons such as C -C chlorinated hydrocarbons, e.g., dichloromethane and dichloroethane and mixtures thereof, may be used as solvents.
  • suitable solvent mixtures are methyl ethyl keytone and methyl isobutyl ketone, methyl ethyl ketone and toluene, dichloromethane and dichloroethane, and propylene and acetone.
  • the preferred solvents are ketones with methyl ethyl ketone being particularly preferred.
  • a particularly preferred solvent mixture is a mixture of methyl ethyl ketone and methyl isobutyl ketone.
  • the petroleum oil stock is fed to the cooling tower 3 at a temperature above its pour and cloud point.
  • the oil may be fed at ambient temperature.
  • higher or lower feed rates can be used.
  • the solvent, orsolvent mixture will be prechilled to a temperature sufficient to permit cooling of the oil to the desiredv temperature.
  • the exact temperature employed will depend upon the amount of oil to be cooled and the amount of solvent to be added to the oil; i.e., the degree of dilution which is sought during the filtration step.
  • the prechilled solvent is added incrementally along the length of the cooling tower so as to maintain an average chilling rate at or below about 8F./minute and preferably between about 1 to about F./minute.
  • the wax content of the oil feed will vary between ten and twenty-five weight percent and the pour and cloud points will range, respectively, between and l70F. and and 175F.
  • a feed rate between and 600 bbl./hour will be used;
  • the amount of solvent added will be sufficient to provide a liquid/solid weight ratio between the range of 5/ l and 20/1 at the dewaxing temperature and a solvent/oil volume ratio between 1.5/1 and 5/1.
  • An essential feature of this invention is the maintenance of a high degree of agitation in at least a portion of the stages during chilling.
  • the degree of agitation must be sufficient to provide substantially instantaneous mixing; i.e., substantially complete mixing of the oil-solvent mixture in one second or less. In this way, the deleterious effects of shock chilling are offset, the chilling rate is more readily controlled and increased filtration rates are obtained.
  • the degree of agitation required in this invention can be achieved by in creasing the agitator RPM when all other mixing variables; e.g., flow rate through the mixer, vessel and agitator design, viscosity of the ingredients, etc. are maintained constant.
  • the degree of agitation required in this invention can be achieved when the modified Reynolds Number, (Perry, Chemical Engineer's Handbook, 3rd, p. 1224, McGraw-l-lill, New York, 1959), N e, which is defined by the equation:
  • liquid viscosity lb./ft. sec. is between about 200 and about 150,000.
  • the dimensionless ratio of cooling tower diameter to agitator diameter is between about l.5/l and about 10/1, and the ratio of the impeller blade length to impeller blade width ranges from about 0.75 to 2 and preferably from about 1 to 1.5.
  • the ratio of the mixing stage height to the diameter of the stage will generally range from about 0.2/1-1/1.
  • a turbine type agitator is preferred; however, other types of agitators such as propeller agitators may be used.
  • the cooling tower may or may not be baffled, but 5" baffled tower is preferred.
  • Each stage will generally contain from about 2-8 bafiles and preferably from 2-4 baffles located about the outer periphery of each stage.
  • the width of the baffles may range from about 5-15 percent of the diameter of the tower.
  • the dimensionless ratio of the cross-section of the restricted flow opening to the cross-section of the tower will be between about 1/20 and about 1/200.
  • the cooling tower of the present invention will be operated at a pressure sufficient to prevent flashing of the solvent. Atmospheric pressure is sufficient when the ketones are employed as solvents; however, superatmospheric pressures are required when low molecular weighthydrocarbons, such as propane, are used.
  • a lubricating oil distillate fraction having a boiling range from about 850 to 950F., a wax content of from about 18 to about 21 wt. percent, and initial pour and cloud points between about 1 l and 120F. and 1 12 and 125F., respectively, is fed from the storage tank 1 through line 2 to the first stage 4(a) of the cooling tower 3.
  • a solvent such as methyl ethyl ketone or a mixture of 55 wt. percent methyl isobutyl ketone and 45 wt. percent methyl ethyl ketone is passed from storage tank 5 through line 6 to the heat exchangers 7 and 8, where the solvent is cooled by conventional means to a temperature between l5 and 25F.
  • cold filtrate from the separator 21 is used to precool the solvent in heat exchanger 7.
  • the filtrate enters through line 24 and leaves through line 26.
  • the solvent is further cooled in heat exchanger 8 with liquid propane or other suitable coolant, entering through line 25 and leaving through line 27. It is preferred that the solvent be prechilled to a temperature which will permit cooling of the oil to a temperature between about 20F. and 25" F. although lower temperatures can be used.
  • the cooled solvent passes from the heat exchanger 8 through line 9 to the manifold 10.
  • the cooling tower is divided into 16 stages, 4, and the manifold consists of 16 parallel solvent inlets 12. The flow rates are adjusted to give the desired temperature drop per stage.
  • Each of the 16 separate stages is provided with an agitator turbine 12 which is turned at a sufficiently high RPM to produce adequate mixing.
  • the oil and solvent entering the first stage 4(a) is substantially instantaneously mixed.
  • the temperature of the total mixture is substantially instantaneously reduced in each stage. In this way, the adverse effects of shock cooling are minimized.
  • the oil-solvent mixture leaves the bottom of the cooling tower as a mixture containing precipitated wax at a temperature ranging from about 0-50F.
  • the solution-wax mixture passes through line 14 to a separating means 15 which is preferably a rotary vacuum filter.
  • the wax-solvent is passed through line 16 to a liquidliquid separating means 19 which is preferably distillation.
  • the wax is recovered through line 18 and the ketone solvent is recovered through line 17.
  • the oilsolvent solution is passed through line 20 to a liquidliquid separating means which is preferably distillation.
  • the dewaxed oil is recovered through line 22 and the mixed ketones solvent is recovered through line 23.
  • the dewaxed oil which now has a reduced pour point and cloud point may be used directly or subjected to further dewaxing by conventional means such as the well known ketone or propane dewaxing methods.
  • Boiling Range 800 to 950F
  • the average chilling rate was 2F./min.
  • the precipitated wax was removed from the oilsolvent solution by filtration.
  • the oil was recovered from solution by distillation.
  • the recovered oil had the following specifications:
  • Boiling Range 800 to 950F
  • the cooling tower employed in this and the following examples was four feet in height and one-half foot in diameter.
  • the solvent inlets were positioned uniformly along the height of the tower at one-half foot intervals.
  • the agitator consisted of 16 impellers positioned along the height of a single shaft. The impeller diameter was 2 inches.
  • the above process has been described in connection with the separation of wax fromoil. However, it may also be used for crystallization and purification of other materials. For example, it can be used to recrystallize slack waxes or petrolatums or with any feed in which there is a crystallizable material which can be separated from the feed on cooling. Thus, it can be used for paraxyle'ne separation, fatty acid purification, dichlorobenzene isomer separation and the like. Additionally it can be used for solvent purification such as benzene, pharmaceutical purification and the like.
  • a process for dewaxing a waxy petroleum oil stock comprising introducing said waxy oil stock into a chilling zone divided into a plurality of stages, introducing a cold dewaxing solvent, into at least a portion of said stages, maintaining a high degree of agitation in a plurality of the solvent-containing stages 56' as to effect a substantially instantaneous mixing of said solvent and 7 is divided into at least 6 agitated stages.
  • cold dewaxing solvent is chosen from the group consisting of ketones having 3 to 6 carbon atoms and their mixtures.
  • cold dewaxing solvent is selected from the group consisting of low molecular weight hydrocarbons and their mixtures.
  • a process for dewaxing a waxy petroleum oil stock comprising introducing said oil stock into a chilling zone divided into at least 6 agitated stages, introducing a cold dewaxing solvent into each of said agitated stages, maintaining a high degree of agitation in each of said stages so as to effect substantially instantaneous mixing of said solvent and waxy oil in each of said agitated stages while cooling the solvent-waxy oil mixture at an average rate of about l8F.
  • a process for dewaxing a waxy petroleum oil stock comprising introducing said oil stock into a chilling zone divided into at least 6 agitated stages, introducing a cold dewaxing solvent into each of said agitated stages, maintaining the degree of agitation in each of said stages between about 200 and 150,000 modified Reynolds Number so as to effect substantially instantaneous mixing of said solvent and oil in each of said agitated stages while cooling said mixture at an average rate of about l8F.
  • a process for dewaxing a waxy lubricating oil stock comprising introducing said petroleum oil stock into the top of a chilling zone divided into between about 6 and 50 agitated stages, introducing a cold dewaxing solvent into each of said stages, maintaining the degree of agitation in each of said stages between about 200 and 150,000 modified Reynolds Number so as to effect substantially instantaneous mixing of said solvent and said oil in each of said agitated stages while cooling said mixture at an average rate of about 1-5F.
  • a process for separating a wax-oil mixture comprising introducing said mixture, at a temperature above its cloud point, into a chilling zone divided into a plurality of stages, introducing a dewaxing solvent into at least a portion of said stages, maintaining a high degree of agitation in a plurality of the solventcontaining stages so as to effect a substantially instantaneous mixing of said solvent and said wax-oil mixture while cooling said mixture as it progresses through said chilling zone thereby precipitating a substantial portion of said wax from said mixture under conditions of said high degree of agitation.
  • a process for dewaxing a waxy petroleum oil stock comprising introducing said petroleum oil stock into a chilling zone divided into a plurality of stages, introducing a dewaxing solvent into a plurality of said stages, maintaining a high degree of agitation in each of said stages so as to effect a substantially instantaneous mixing of said solvent and said oil while cooling said solvent-oil mixture as it progresses through said chilling zone thereby precipitating a substantial portion of the wax from said mixture under conditions of said high degree of agitation, separating precipitated wax from said solvent-oil mixture and recovering a petroleum oil stock having a reduced wax content from said mixture.
  • a process for dewaxing a waxy petroleum oil stock comprising introducing said petroleum oil stock into a chilling zone divided into a plurality of stages, in-
  • dewaxing solvent comprises a mixture of methylethyl ketone and toluene.
  • dewaxing solvent comprises a mixture of methylethyl ketone and toluene.
  • dewaxing solvent comprises a mixture of methylethyl ketone and toluene.

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)
US00129973A 1971-03-31 1971-03-31 Dewaxing process Expired - Lifetime US3773650A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US12997371A 1971-03-31 1971-03-31
JP4418972A JPS5522520B2 (enrdf_load_stackoverflow) 1971-03-31 1972-05-02
FR7215921A FR2182704B1 (enrdf_load_stackoverflow) 1971-03-31 1972-05-04

Publications (1)

Publication Number Publication Date
US3773650A true US3773650A (en) 1973-11-20

Family

ID=27249850

Family Applications (1)

Application Number Title Priority Date Filing Date
US00129973A Expired - Lifetime US3773650A (en) 1971-03-31 1971-03-31 Dewaxing process

Country Status (3)

Country Link
US (1) US3773650A (enrdf_load_stackoverflow)
JP (1) JPS5522520B2 (enrdf_load_stackoverflow)
FR (1) FR2182704B1 (enrdf_load_stackoverflow)

Cited By (49)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2855520A1 (de) * 1977-12-27 1979-07-05 Exxon Research Engineering Co Verfahren zum entparaffinieren von paraffinhaltigem oel
US4216075A (en) * 1978-12-28 1980-08-05 Ryan Douglas G Combination dewaxing process
EP0027722A3 (en) * 1979-10-19 1981-06-10 Exxon Research And Engineering Company Process for dewaxing hydrocarbons employing low-speed scraped-surface chillers
EP0036460A1 (en) * 1980-03-21 1981-09-30 Exxon Research And Engineering Company A continuous process for dewaxing waxy oil using dewaxing solvent and auto-refrigerant, and apparatus therefor
US4314886A (en) * 1978-12-28 1982-02-09 Exxon Research & Engineering Co. Mechanically agitated liquid-vapor contacting apparatus
US4334978A (en) * 1979-10-19 1982-06-15 Exxon Research & Engineering Co. Dewaxing and wax filterability by reducing scraper speed in scraped surface chilling units
EP0088603A1 (en) * 1982-03-08 1983-09-14 Exxon Research And Engineering Company Process for solvent dewaxing hydrocarbon oil using methyl tertiary butyl ether
US4432866A (en) * 1981-10-21 1984-02-21 Exxon Research And Engineering Co. Membrane separation process
US4441987A (en) * 1981-03-20 1984-04-10 Exxon Research & Engineering Company Dewaxing process using agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
US4477333A (en) * 1982-09-29 1984-10-16 Exxon Research And Engineering Co. Dewaxing by a combination centrifuge/catalytic process including solvent deoiling
EP0127364A1 (en) * 1983-05-13 1984-12-05 Exxon Research And Engineering Company Adhesive system for production of spiral wound membrane elements for use in organic fluid mixture separations
US4502787A (en) * 1981-03-20 1985-03-05 Exxon Research & Engineering Co. Agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
FR2558846A1 (fr) * 1984-01-31 1985-08-02 Exxon Research Engineering Co Procede et appareil pour le deparaffinage d'huiles hydrocarbonees
US4541917A (en) * 1983-12-19 1985-09-17 Exxon Research And Engineering Co. Modified deoiling-dewaxing process
US4695363A (en) * 1986-05-27 1987-09-22 Exxon Research And Engineering Company Wax crystal modification using dewaxing aids under agitated conditions
US4697426A (en) * 1986-05-29 1987-10-06 Shell Western E&P Inc. Choke cooling waxy oil
US4702758A (en) * 1986-05-29 1987-10-27 Shell Western E&P Inc. Turbine cooling waxy oil
US4728413A (en) * 1984-09-24 1988-03-01 Exxon Research And Engineering Company Agitated dewaxing employing modified agitator means
JPH0214288A (ja) * 1989-04-13 1990-01-18 Exxon Res & Eng Co 連続式自己冷却型脱ワックス装置
US4952303A (en) * 1985-07-10 1990-08-28 Mobil Oil Corp. Process for preparing a very high quality lube base stock oil
US5098550A (en) * 1989-10-06 1992-03-24 Rohm Gmbh Method for dewaxing waxy petroleum products
US5167847A (en) * 1990-05-21 1992-12-01 Exxon Research And Engineering Company Process for producing transformer oil from a hydrocracked stock
US5196116A (en) * 1991-02-11 1993-03-23 University Of Arkansas Process for petroleum - wax separation at or above room temperature
WO1995007327A1 (en) * 1993-09-10 1995-03-16 Exxon Research & Engineering Company Controlling chilling tower profile for dilution chilling dewaxing of 600n waxy oil
US5474668A (en) * 1991-02-11 1995-12-12 University Of Arkansas Petroleum-wax separation
US5620588A (en) * 1991-02-11 1997-04-15 Ackerson; Michael D. Petroleum-wax separation
US6656366B1 (en) 1999-07-12 2003-12-02 Halliburton Energy Services, Inc. Method for reducing solids buildup in hydrocarbon streams produced from wells
US6773578B1 (en) 2000-12-05 2004-08-10 Chevron U.S.A. Inc. Process for preparing lubes with high viscosity index values
US20050077208A1 (en) * 2003-10-14 2005-04-14 Miller Stephen J. Lubricant base oils with optimized branching
US20050077209A1 (en) * 2003-10-14 2005-04-14 Miller Stephen J. Processes for producing lubricant base oils with optimized branching
US20050086311A1 (en) * 2003-03-03 2005-04-21 Noel Enete Regulating self-disclosure for video messenger
US20050139514A1 (en) * 2003-12-30 2005-06-30 Chevron U.S.A. Inc. Hydroisomerization processes using sulfided catalysts
US20050139513A1 (en) * 2003-12-30 2005-06-30 Chevron U.S.A. Inc. Hydroisomerization processes using pre-sulfided catalysts
US20050261146A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Processes for making lubricant blends with low brookfield viscosities
US20050261147A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
US20050258078A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Processes for making lubricant blends with low brookfield viscosities
US20050261145A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
WO2006055500A1 (en) 2004-11-15 2006-05-26 Exxonmobil Research And Engineering Company A method for making a lubricating oil with improved low temperature properties
US20060113512A1 (en) * 2004-12-01 2006-06-01 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US20060113216A1 (en) * 2004-12-01 2006-06-01 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
EP1688476A1 (en) 2005-01-31 2006-08-09 Chevron Oronite Company LLC Lubricating base oil compositions and methods for improving fuel economy in an internal combustion engine using same
US20060199743A1 (en) * 2005-03-03 2006-09-07 Chevron U.S.A. Inc. Polyalphaolefin & fischer-tropsch derived lubricant base oil lubricant blends
US20060205610A1 (en) * 2005-03-11 2006-09-14 Chevron U.S.A. Inc. Processes for producing extra light hydrocarbon liquids
EP1927647A1 (en) 2006-11-30 2008-06-04 Chevron Oronite Company LLC Traction coefficient reducing lubricating oil composition
WO2008051492A3 (en) * 2006-10-23 2008-07-10 Exxonmobil Res & Eng Co Method for on-line monitoring of wax crystallization
US20080255012A1 (en) * 2007-02-08 2008-10-16 Chevron U.S.A. Inc. Automatic transmission fluid
US20090005275A1 (en) * 2007-06-28 2009-01-01 Chevron U.S.A. Inc. Power steering fluid
US20090149357A1 (en) * 2007-12-10 2009-06-11 Chevron U.S.A. Inc. Lubricant composition
US11098967B2 (en) * 2007-10-10 2021-08-24 Prime Datum, Inc. Integrated fan drive system for cooling tower

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL162129C (nl) * 1967-09-08 Exxon Research Engineering Co Werkwijze voor het ontparaffineren van petroleumolien.

Cited By (70)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2413463A1 (fr) * 1977-12-27 1979-07-27 Exxon Research Engineering Co Procede pour le deparaffinage d'huile de recuperation
US4169039A (en) * 1977-12-27 1979-09-25 Exxon Research & Engineering Co. Recovering useful oil from wax filter hot washings and dumped slurry
DE2855520A1 (de) * 1977-12-27 1979-07-05 Exxon Research Engineering Co Verfahren zum entparaffinieren von paraffinhaltigem oel
US4216075A (en) * 1978-12-28 1980-08-05 Ryan Douglas G Combination dewaxing process
US4314886A (en) * 1978-12-28 1982-02-09 Exxon Research & Engineering Co. Mechanically agitated liquid-vapor contacting apparatus
EP0027722A3 (en) * 1979-10-19 1981-06-10 Exxon Research And Engineering Company Process for dewaxing hydrocarbons employing low-speed scraped-surface chillers
US4334978A (en) * 1979-10-19 1982-06-15 Exxon Research & Engineering Co. Dewaxing and wax filterability by reducing scraper speed in scraped surface chilling units
EP0036460A1 (en) * 1980-03-21 1981-09-30 Exxon Research And Engineering Company A continuous process for dewaxing waxy oil using dewaxing solvent and auto-refrigerant, and apparatus therefor
US4502787A (en) * 1981-03-20 1985-03-05 Exxon Research & Engineering Co. Agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
US4441987A (en) * 1981-03-20 1984-04-10 Exxon Research & Engineering Company Dewaxing process using agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
US4432866A (en) * 1981-10-21 1984-02-21 Exxon Research And Engineering Co. Membrane separation process
EP0088603A1 (en) * 1982-03-08 1983-09-14 Exxon Research And Engineering Company Process for solvent dewaxing hydrocarbon oil using methyl tertiary butyl ether
US4477333A (en) * 1982-09-29 1984-10-16 Exxon Research And Engineering Co. Dewaxing by a combination centrifuge/catalytic process including solvent deoiling
EP0127364A1 (en) * 1983-05-13 1984-12-05 Exxon Research And Engineering Company Adhesive system for production of spiral wound membrane elements for use in organic fluid mixture separations
US4541917A (en) * 1983-12-19 1985-09-17 Exxon Research And Engineering Co. Modified deoiling-dewaxing process
FR2558846A1 (fr) * 1984-01-31 1985-08-02 Exxon Research Engineering Co Procede et appareil pour le deparaffinage d'huiles hydrocarbonees
US4728413A (en) * 1984-09-24 1988-03-01 Exxon Research And Engineering Company Agitated dewaxing employing modified agitator means
US4952303A (en) * 1985-07-10 1990-08-28 Mobil Oil Corp. Process for preparing a very high quality lube base stock oil
US4695363A (en) * 1986-05-27 1987-09-22 Exxon Research And Engineering Company Wax crystal modification using dewaxing aids under agitated conditions
US4702758A (en) * 1986-05-29 1987-10-27 Shell Western E&P Inc. Turbine cooling waxy oil
US4697426A (en) * 1986-05-29 1987-10-06 Shell Western E&P Inc. Choke cooling waxy oil
JPH0214288A (ja) * 1989-04-13 1990-01-18 Exxon Res & Eng Co 連続式自己冷却型脱ワックス装置
US5098550A (en) * 1989-10-06 1992-03-24 Rohm Gmbh Method for dewaxing waxy petroleum products
US5167847A (en) * 1990-05-21 1992-12-01 Exxon Research And Engineering Company Process for producing transformer oil from a hydrocracked stock
US5620588A (en) * 1991-02-11 1997-04-15 Ackerson; Michael D. Petroleum-wax separation
US5474668A (en) * 1991-02-11 1995-12-12 University Of Arkansas Petroleum-wax separation
US5196116A (en) * 1991-02-11 1993-03-23 University Of Arkansas Process for petroleum - wax separation at or above room temperature
US5853564A (en) * 1991-02-11 1998-12-29 University Of Arkansas Petroleum-wax separation
US6024862A (en) * 1991-02-11 2000-02-15 Advanced Refining Technologies, Inc. Petroleum-wax separation
WO1995007327A1 (en) * 1993-09-10 1995-03-16 Exxon Research & Engineering Company Controlling chilling tower profile for dilution chilling dewaxing of 600n waxy oil
US5401383A (en) * 1993-09-10 1995-03-28 Exxon Research & Engineering Co. Controlling chilling tower profile for dilution chilling dewaxing of 600N waxy oil
US6656366B1 (en) 1999-07-12 2003-12-02 Halliburton Energy Services, Inc. Method for reducing solids buildup in hydrocarbon streams produced from wells
US6773578B1 (en) 2000-12-05 2004-08-10 Chevron U.S.A. Inc. Process for preparing lubes with high viscosity index values
US20050086311A1 (en) * 2003-03-03 2005-04-21 Noel Enete Regulating self-disclosure for video messenger
US20050077208A1 (en) * 2003-10-14 2005-04-14 Miller Stephen J. Lubricant base oils with optimized branching
US7018525B2 (en) 2003-10-14 2006-03-28 Chevron U.S.A. Inc. Processes for producing lubricant base oils with optimized branching
US20050077209A1 (en) * 2003-10-14 2005-04-14 Miller Stephen J. Processes for producing lubricant base oils with optimized branching
US20050139514A1 (en) * 2003-12-30 2005-06-30 Chevron U.S.A. Inc. Hydroisomerization processes using sulfided catalysts
US20050139513A1 (en) * 2003-12-30 2005-06-30 Chevron U.S.A. Inc. Hydroisomerization processes using pre-sulfided catalysts
US7273834B2 (en) 2004-05-19 2007-09-25 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
US20050261146A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Processes for making lubricant blends with low brookfield viscosities
US20050261147A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
US20050258078A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Processes for making lubricant blends with low brookfield viscosities
US20050261145A1 (en) * 2004-05-19 2005-11-24 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
US7572361B2 (en) 2004-05-19 2009-08-11 Chevron U.S.A. Inc. Lubricant blends with low brookfield viscosities
US7473345B2 (en) 2004-05-19 2009-01-06 Chevron U.S.A. Inc. Processes for making lubricant blends with low Brookfield viscosities
US7384536B2 (en) 2004-05-19 2008-06-10 Chevron U.S.A. Inc. Processes for making lubricant blends with low brookfield viscosities
WO2006055500A1 (en) 2004-11-15 2006-05-26 Exxonmobil Research And Engineering Company A method for making a lubricating oil with improved low temperature properties
US20060113512A1 (en) * 2004-12-01 2006-06-01 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US7252753B2 (en) 2004-12-01 2007-08-07 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US7510674B2 (en) 2004-12-01 2009-03-31 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US20060113216A1 (en) * 2004-12-01 2006-06-01 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
EP1688476A1 (en) 2005-01-31 2006-08-09 Chevron Oronite Company LLC Lubricating base oil compositions and methods for improving fuel economy in an internal combustion engine using same
US7476645B2 (en) 2005-03-03 2009-01-13 Chevron U.S.A. Inc. Polyalphaolefin and fischer-tropsch derived lubricant base oil lubricant blends
US20060199743A1 (en) * 2005-03-03 2006-09-07 Chevron U.S.A. Inc. Polyalphaolefin & fischer-tropsch derived lubricant base oil lubricant blends
US7655605B2 (en) 2005-03-11 2010-02-02 Chevron U.S.A. Inc. Processes for producing extra light hydrocarbon liquids
US20060205610A1 (en) * 2005-03-11 2006-09-14 Chevron U.S.A. Inc. Processes for producing extra light hydrocarbon liquids
US7981270B2 (en) 2005-03-11 2011-07-19 Chevron U.S.A. Inc. Extra light hydrocarbon liquids
US20060201852A1 (en) * 2005-03-11 2006-09-14 Chevron U.S.A. Inc. Extra light hydrocarbon liquids
WO2008051492A3 (en) * 2006-10-23 2008-07-10 Exxonmobil Res & Eng Co Method for on-line monitoring of wax crystallization
US20100065469A1 (en) * 2006-10-23 2010-03-18 Palmer Thomas R Method for on-line monitoring of wax crystallization
EP2080021A4 (en) * 2006-10-23 2014-07-09 Exxonmobil Res & Eng Co METHOD FOR ONLINE MONITORING OF CRYSTALLIZATION OF A WAX
US8029661B2 (en) * 2006-10-23 2011-10-04 Exxonmobil Research And Engineering Company Method for on-line monitoring of wax crystallization
EP1927647A1 (en) 2006-11-30 2008-06-04 Chevron Oronite Company LLC Traction coefficient reducing lubricating oil composition
US20080255012A1 (en) * 2007-02-08 2008-10-16 Chevron U.S.A. Inc. Automatic transmission fluid
US20110028362A1 (en) * 2007-02-08 2011-02-03 Chevron U.S.A. Inc. Automatic Transmission Fluid
US20090005275A1 (en) * 2007-06-28 2009-01-01 Chevron U.S.A. Inc. Power steering fluid
US11098967B2 (en) * 2007-10-10 2021-08-24 Prime Datum, Inc. Integrated fan drive system for cooling tower
US7956018B2 (en) 2007-12-10 2011-06-07 Chevron U.S.A. Inc. Lubricant composition
US20090149357A1 (en) * 2007-12-10 2009-06-11 Chevron U.S.A. Inc. Lubricant composition

Also Published As

Publication number Publication date
JPS4910904A (enrdf_load_stackoverflow) 1974-01-30
JPS5522520B2 (enrdf_load_stackoverflow) 1980-06-17
FR2182704B1 (enrdf_load_stackoverflow) 1976-10-29
FR2182704A1 (enrdf_load_stackoverflow) 1973-12-14

Similar Documents

Publication Publication Date Title
US3773650A (en) Dewaxing process
US3775288A (en) Combination of dilution chilling with scraped surface chilling in dewaxing lubricating oils
US4140620A (en) Incremental dilution dewaxing process
US3458430A (en) Separation of hydrocarbon wax from mineral oil using dewaxing aids
US4013542A (en) Partial predilution dilution chilling
US4146461A (en) Dilution chilling dewaxing by modification of tower temperature profile
US4441987A (en) Dewaxing process using agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
US3681230A (en) Immiscible filtration of dilution chilled waxy oils
US3642609A (en) Dewaxing waxy oil by dilution chilling
US4115241A (en) Solvent dewaxing process
US3644195A (en) Solvent dewaxing-deoiling process
US4502787A (en) Agitated heat exchanger to chill solvent-oil and wax slurry to wax filtration temperature
EP0458476A2 (en) Solvent dewaxing of lubricating oils
US2361503A (en) Wax-oil separation
US4111790A (en) Dilution chilling dewaxing solvent
US3850740A (en) Partial predilution dilution chilling
US4444648A (en) Solvent dewaxing with methyl tertiary butyl ether
US2642377A (en) Dewaxing process
US4145275A (en) Dilchill dewaxing using wash filtrate solvent dilution
US3779894A (en) Immiscible injection of solvent in dilution chilling of waxy oils
US4115245A (en) Solvent dewaxing process
US4354921A (en) Solvent dewaxing process
US4088565A (en) Solvent dewaxing process
US4115244A (en) Solvent dewaxing process
US3972802A (en) Immiscible coolant in propylene-acetone dewaxing