US3629096A - Production of technical white mineral oil - Google Patents

Production of technical white mineral oil Download PDF

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Publication number
US3629096A
US3629096A US647628A US3629096DA US3629096A US 3629096 A US3629096 A US 3629096A US 647628 A US647628 A US 647628A US 3629096D A US3629096D A US 3629096DA US 3629096 A US3629096 A US 3629096A
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Prior art keywords
hydrogen
alumina
catalyst
oil
platinum
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Expired - Lifetime
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US647628A
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English (en)
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Joseph M Divijak Jr
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Atlantic Richfield Co
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Atlantic Richfield Co
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Priority claimed from CA113,786A external-priority patent/CA953233A/en
Priority claimed from DE19712131227 external-priority patent/DE2131227A1/de
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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • C10G45/52—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing platinum group metals or compounds 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/10—Lubricating oil
    • 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
    • C10G2400/14—White oil, eating oil

Definitions

  • This invention relates to a process for the'production of technical grade white mineral oil from raw, waxy mineral oil distillates. More particularly, this invention concerns a hydrorefining, hydroisomerization-hydrocracking, aromatic saturation, catalytic conversion process for the production of technical grade white mineral oil in increased yields and at reduced operating costs.
  • the present invention concerns a hydrorefining, hydroisomerization-hydrocracking, aromatic saturation process wherein a raw, waxy, lubricating oil distillate having a high pour point, and a high aromatic content is converted into a technical grade white mineral oil in increased yields and at reduced operating coats.
  • the raw, waxy, lubricating oil distillate is contacted in a first stage 'with hydrogen in the presence of a desulfurization-denitrogenation type catalyst under hydrorefining conditions and treated in a second stage with hydrogen in the presence of a hydroisomerizationhydrocracking catalyst.
  • the oil of lubricating viscosity in the second stage product is further contacted in a third stage with hydrogen under aromatic saturation conditions to produce high quality technical grade white mineral oil.
  • the mineral lubricating oil distillates to be treated by the process of the present invention are raw, waxy lubricating oil distillates which may even represent the complete distillate lubricating oil fraction derived from a waxy crude oil.
  • the lubricating oil distillates useful as feedstocks in the present invention often possess a viscosity in the range of about 35 to 90 SUS at 2 F., an aromatic carbon content of about to 30 percent, a pour point of atleast about 70 F., and boil primarily in the range of about 600 to 1,200 F.
  • the hydrorefining treatment in the first stage of the present process is conducted at temperatures of about 600 to 800 F., preferably about 675 to 725 F
  • the other reaction conditions generally can include pressures of about 500 to 3,000 p.s.i.g., preferably about 2,000 to 3,000 p.s.i.g., weight hourly space velocities (WHSV) of about 0.2 to 2, preferably about 0.25 to 0.5; and molecular hydrogen to feed oil ratios of about 1,000 to 5,000 SCF/B, preferably about 1,500 to 2,500 SCF/B.
  • WHSV weight hourly space velocities
  • the hydrogenated oil from the first hydrogenation stage is subjected to a second hydrogenation operation in which the catalyst is such that hydroisomerization and hydrocracking are effected.
  • temperatures in the second stage range from about 600 to 950 F., with temperatures of about 650 to 800 F. being preferred.
  • Other reaction conditions can include pressures of about 500 to 3,000 p.s.i.g., preferably about 2,000 to 3,000 p.s.i.g., weight hourly space velocities of about 0.25 to 2, preferably about 0.25 to 0.5, and molecular hydrogen to feed oilratio of about 1,000 to 5,000 SCF/B, preferably about 2,000 to 3,000 SCF/B.
  • the aromatic saturation of the product of lubricating viscosity made in the second stage is in the third stage of the operation of this invention, and is conducted at a temperature of about 450 to 700 F., preferably about 550 to 600 F.
  • Other reaction conditions can include a pressure of about 500 to 3,000 p.s.i.g., preferably about 2,000 to 3,000 p.s.i.g., a weight hourly space velocity of about 0.2 to 2, preferably about 0.25 to 0.5, and a hydrogen to feed oil rate of about 1,000 to 5,000 SCF/B, preferably about 2,000 to 3,000 SCF/B.
  • the desulfurization-denitrogenation type catalysts used in the first stage of the present process can be the sulfur-resistant, nonprecious metal hydrogenation catalysts, such as those conventionally employed in the hydrogenation of heavy petroleum oils.
  • suitable catalytic ingredients are tin, vanadium, members of Group VlB in the Periodic Table, i.e. chromium, molybdenum and tungsten, and metals of the iron group, i.e. iron, cobalt and nickel. These metals are present in catalytically effective amounts, for instance, about 2 to 30 weight percent, and may be in elemental form or in combined form such as the oxides or sulfides, the sulfides being preferred.
  • Such mixtures or compounds are nickel molybdate, tungstate or chromate (or thiomolybdate, thio-tungstate or thiochromate) or mixtures of nickel or cobalt oxides with molybdenum, tungsten or chromium oxides,
  • these catalytic ingredients are generally employed while disposed upon a suitable carrier of the solid oxide refractory type, e.g., a predominantly calcined or activated alumina or other base exerting little cracking effect.
  • a suitable carrier of the solid oxide refractory type e.g., a predominantly calcined or activated alumina or other base exerting little cracking effect.
  • Commonly employed catalysts have about 1 to 10 percent of an iron group metal and 5 to 25 percent of a Group VlB metal (calculated as the oxide).
  • the catalyst is nickel molybdate supported on alumina.
  • Such preferred catalyst can be prepared, for instance, by the method described in U.S. Pat. No. 2,93
  • the platinum group metal-containing hydroisomerizationhydrocracking catalyst used in the second stage of the method of the present invention is not normally sulfur-resistant and contains a major amount of an amorphous silica-alumina composite, containing for instance, about 5 to 45, preferably about 10 to 20, weight percent alumina on a dry basis; about 3 to 25, preferably about 5 to 10, weight percent of a hydrogenexchanged crystalline alumino-silicate having a silica-to-alumina mole ratio greater than 3:1; and a catalytic amount, say about 0.1 to 5, preferably about 0.3 to 2, weight percent of a platinum group metal.
  • an amorphous silica-alumina composite containing for instance, about 5 to 45, preferably about 10 to 20, weight percent alumina on a dry basis; about 3 to 25, preferably about 5 to 10, weight percent of a hydrogenexchanged crystalline alumino-silicate having a silica-to-alumina mole ratio greater than 3:1; and a catalytic
  • the catalyst may also contain a small amount, e.g., less than about 1 weight percent of halide such as chloride or fluoride. If desired, a small amount, for instance about 5 to 20 or more weight percent of a suitable binder material, for example, alumina hydrogel, may be added to the second stage catalyst composition especially if the catalyst is formed by extrusion.
  • a suitable binder material for example, alumina hydrogel
  • the platinum group metals include such group VlIl metals as, for example, platinum, palladium, rhodium, or iridium.
  • the platinum group metal may be present in the metallic form or as a sulfide, oxide or other combined form, The metal may interact with other constituents of the catalyst, but if during use the platinum group metal is present in the metallic form, then it is preferred that it be so finely divided that it is not detectable by X-ray defraction means, i.e. that it exists as crystallites of less than about 50 A. in size.
  • the amorphous silica-alumina composite employed in the second stage catalyst of the process of the invention is usually synthetically precipitated.
  • the silica-alumina can be prepared by any desired method and several procedures are known in the art.
  • a hydrogel can be prepared by coprecipitation or sequential precipitation by either component being the initial material precipitated with at least the principal part of the silica or alumina being made in the presence of the other, Generally the alumina is precipitated in the presence of a silica gel.
  • the silica-alumina hydrogel be made by forming a silica hydrogel by precipitation from an alkali metal silicate solution and an acid such as sulfuric acid. Then alum solution may be added to the silica hydrogel slurry.
  • the alumina is precipitated by raising the pH into the alkaline range by the addition of an aqueous sodium aluminate solution or by the addition of a base such as ammonium hydroxide.
  • a base such as ammonium hydroxide.
  • Other techniques for preparing the silica-alumina are well known in the are, and these techniques may be used.
  • the silica-alumina is present in xerogel or catalytically active form due to treatment at elevated temperatures as by calcination of the hydrogel.
  • the crystalline aluminosilicate component of the second stage catalyst may be synthetic or naturally occurring and has a pore size of about 8 to 15 A., preferably about 10 t 14 A. Usually, with a given material, the pores are relatively uniform in size and often the crystalline alumino-silicate particles used to make the catalyst are primarily less than about 15 microns in size, preferably less than about microns. 1n the crystalline aluminosilicate, the silica-to-alumina mole ratio is greater that 3:1 and is usually not above about 12:1, preferably being about 4 to 6:1.
  • the aluminosilicate is at least about 50 percent, preferably at least about 75 percent, hydrogenexehanged.
  • Hydrogen exchange is commonly carried out by exchange of the cations of the synthetic or naturally occurring aluminosilicates with ammonium ions, for instance through contact with an aqueous solution of ammonium chloride or other water-soluble ammonium compound and subsequently calcining the aluminosilicate.
  • One method of preparing the second stage catalyst is by combining the silica-alumina hydrogel and the hydrogenexchanged crystalline aluminosilicate and drying the mixture, for instance at temperatures of about 230 to 600 F., to con vert the silica-alumina hydrogel to the xerogel form.
  • the crystalline aluminosilicate may, if desired, be hydrogenexchanged after it is combined with the silica-alumina hydrogel.
  • the dried material can be calcined, for instance, at a temperature of the order of about 700 to 1500 F., preferably about 800 to 1,100" F.
  • the platinum group metal may be added before or after the calcination, by, for example, ion exchange or impregnation, 1n any event, after the platinum group metal is added, the catalyst can be dehydrated and activated at the calcination temperature described above.
  • An available method for adding the platinum group metal by ion exchange comprises treating the silica-aluminacrystalline alumino-silicate mixture with an aqueous solution containing complex water-soluble, metal-amine cations, both organic and inorganic, of the metal to be deposited in the crystal structure. These complex cations ion-exchange with the cations present in the crystalline aluminosilicate.
  • the exchange material is then removed from the solution, dried and activated or calcined, for example, by heating the material up to a temperature of about 250 C. in a flowing stream ofinert dry gas or vacuum. The activation may be effected at a temperature below the temperature at which the complex cations are destroyed.
  • the activated material may then be subjected to heat treatment to a temperature not exceeding about 650 C. and preferably not exceeding about 500 C. in vacuum or inert atmosphere whereby the complex cation is destroyed and the platinum group metal is reduced in the material.
  • heat treatment to be insufficient to reduce the metal of the complex cations to the elemental state, chemical reduction either alone or in combination with thermal reduction may be employed.
  • Alkali metals such sodium are suitable reducing agents for this purpose. Throughout the operation excessive temperatures and extremes of acidity are to be avoided since they may tend to destroy the crystal structure ofthe silica-alumina-crystalline aluminosilicate mixture.
  • the platinum group metal may also be added by impregnation.
  • the silica-alumina-crystalline aluminosilicate mixture for example, either with or without previous evacuation, may be soaked in either a dilute or concentrated solution, usually aqueous chloroplatinic acid, ammonium hexathiocyanoplatinate (1V) or hexathiocyanate platinic acid, often in an amountjust sufficient to wet the material and be completely absorbed. Also, ifdesired, the solution may be incorporated into the silica-a1umina-crystalline aluminosilicate during the formation ofthe latter.
  • the catalyst can, if desired, be formed into macrosized particles by -inch or extruding. Generally, these particles are about l/32 inch to k inch in diameter and about l/16-inch to l-inch or more in length. Although these macrosized particles are usually formed after dehydration and before calcination, this, of course is optional and can be done at any time found most convenient.
  • the catalyst employed in the third, or aromatic-saturation stage of the present invention is a platinum group metal-containing hydrogenation catalyst.
  • This catalyst like the catalysts of the second stage, is distinguished from the catalysts of the first stage in that it is not normally considered to be sulfur-resistant.
  • the catalyst includes catalytically effective amounts of the platinum group metals mentioned above. Often, the platinum group metal is present in an amount, for example, of about 0,01 to 2 weight percent, preferably about 0.1 to 1 weight percent.
  • the platinum group metal may be present in the metallic form or as a sulfide, oxide, or other combined form.
  • the metal may interact with other constituents of the catalyst but if during use the platinum group metal is present in metallic form, then it is preferred that it be so finely divided that it is not detectable by X-ray diffraction means, i.e. that it exists as crystallites ofless than about 50 A. size. Of the platinum group metals, platinum is preferred.
  • the catalysts employed in the third stage of the process of the invention can be prereduced prior to use by heating in the presence of hydrogen, generally at temperatures of about 600 to 800 F.
  • the preferred supports have no substantial cracking effect on the hydrocarbon feeds.
  • the support is composed predominantly of alumina of the activated or calcined type.
  • the alumina base is usually the major component of the catalyst, generally constituting at least about 75 weight percent on the basis of the catalyst and preferably at least about to 99.8 percent.
  • the alumina catalyst base can be an activated or gamma family alumina, especially gamma or eta alumina, such as those derived by calcination of amorphous hydrous alumina, alumina monohydrate, alumina trihydrate or their mixtures.
  • a catalyst base advantageously used is a mixture predominating in, or containing a major proportion of, for instance about 65 to weight percent, of one or more of the alumina trihydrates, bayerite, nordstandite or gibbsite, and about 5 to 35 weight percent of alumina monohydrate (boehmite), amorphous hydrous alumina or their mixtures.
  • the alumina base can contain small amounts of other solid oxides such as silica, magnesia, natural or activated clays (such as kaolinite, montmorillonite, halloysite, etc.), Titania zirconia, etc., or their mixtures.
  • platinum group metal to the alumina or other solid refractory type carrier
  • the platinum-group metal hydrogenation catalysts used in the third stage of the process of the invention may be employed in the form of macrosized particles generally having a diameter of about 1/32-inch to zfi-inch and a length of about l/l 6-inch to linch or more.
  • the catalyst which contained 2.3 percent nickel and 15.6 percent molybdenum as the oxide, was pretreated with hydrogen sulfide at 350 F.
  • the hydrotreated product thus formed was flashed to remove light gaseous products and further treated in a second stage at a temperature of 750 F., a pressure of 2,500 p.s.i.g., a weight hourly space velocity of 0.35 and a hydrogen rate of 2,500 SCF/B of feed in the presence of a calcined platinum-containing, silica-alumina-crystalline aluminosilicate extrudate catalyst.
  • the catalyst contained about 0.5 weight percent platinum, about 7 weight percent of about 90 percent hydrogen-exchanged crystalline aluminosilicate having a pore size of about 13 A. and a silica-to-alumina mole ratio of about 4 to 1, about 82.5 weight percent silica-alumina xerogel containing about 13 weight percent alumina, and about weight alumina added as a hydrogel.
  • the effluent product from the second stage was steam stripped to remove hydrocracked components boiling below the lubricating oil range, and contacted with hydrogen at a temperature of 550 F., a pressure of 2,500 p.s.i.g., a weight hourly space velocity of 0.25 and a hydrogen rate of 2,7500 SCF/B of feed in the presence of a platinum on alumina catalyst containing 0.6 weight percent platinum.
  • Technical grade white mineral oil was recovered in a yield of about 30 percent by weight.
  • a process of producing a technical white mineral oil which comprises contacting a raw, waxy mineral lubricating oil distillate having a viscosity of about 35 to 90 SUS at 210 F., an aromatic carbon content of about 15 to 30 percent, a pour point of at least about 70 F., and boiling primarily in the range of about 600 to 1,200 F., with hydrogen in the presence of a sulfur-resistant hydrogenation catalyst at a temperature of about 600 to 800 F.
  • a hydroisomerization-hydrocracking catalyst comprising a major amount of amorphous silica-alumina composite containing about 5 to 45 weight percent alumina on a dry basis about 3 to 25 weight percent of an at least about 50 percent hydrogen-exchanged crystalline aluminosilicate having a pore size of about 8 to 15 A., and a silica-to-alumina mole ratio greater than 3:1.
  • a platinum group metal at a temperature of about 600 to 950 F., removing components boiling below the lubricating oil range from the resulting product, and further contacting resulting hydroisomerized-hydrocracked product fraction of lubricating viscosity with hydrogen in the presence of a hydrogenation catalyst comprising a platinum group metal on a support having no substantial cracking effect on said hydroisomerization-hydrocracked product fraction, at a temperature of about 450 to 700 F. to saturate aromatics and produce technical white mineral oil.
  • a process of producing a technical white mineral oil which comprises contacting in a first stage a raw, waxy mineral lubricating oil distillate having a viscosity of about 35 to 90 SUS at 210 F., an aromatic carbon content of about 15 to 30 percent, and a pour point of at least about F., and boiling primarily in the range of about 600 to 1,200 F., with hydrogen in the presence of a catalytic amount of a sulfided nickel molybdate supported on alumina catalyst at a temperature of about 675 to 725 F., a pressure of about 2,000 to 3,000 p.s.i.g., a weight hourly space velocity of about 0.25 to 0.5 and a hydrogen feed rate of about 1,500 to 2,500 SCF/B to provide a hydrorefined oil, contacting said hydrorefined oil in a second stage with hydrogen at a temperature of about 650 to 800 F.
  • a hydroisomerizationhydrocracking catalyst which comprises a major amount of amorphous silica-alumina composite containing about 10 to 20 weight percent alumina on a dry basis, about 5 to 10 weight percent of at least about percent hydrogen-exchanged crystalline aluminosilicate having a pore size of 10 to 14 A., a crystal size of less than about 10 microns and a silica-to-alumina mole ratio of about 4 to 6:1, and about 0.3 to 2 weight percent of platinum, removing components boiling below the lubricating oil range from the resulting product, and further contacting the fraction of the oil of lubricating viscosity from said second stage with hydrogen in the presence of a platinumalumina catalyst containing about 0.1 to 1 weight percent platinum at a temperature of about 550 to 600 F., a pressure of about 2,000 to 3,000 p.s.i.g., a weight hourly space velocity of about 0.25 to 0.5 and a hydrogen to feed oil rate of about 2,000 to

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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)
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US647628A 1967-06-21 1967-06-21 Production of technical white mineral oil Expired - Lifetime US3629096A (en)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
US64762867A 1967-06-21 1967-06-21
CA113,786A CA953233A (en) 1967-06-21 1971-05-25 Production of technical white mineral oil
GB2779571 1971-06-14
NL7108226A NL7108226A (enrdf_load_stackoverflow) 1967-06-21 1971-06-15
DE19712131227 DE2131227A1 (de) 1971-06-18 1971-06-18 Verfahren zur Herstellung von Weissoel
FR7122475A FR2142583B1 (enrdf_load_stackoverflow) 1967-06-21 1971-06-21
BE768821A BE768821A (fr) 1967-06-21 1971-06-21 Procede de production d'huile minerale blanche

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US3629096A true US3629096A (en) 1971-12-21

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US (1) US3629096A (enrdf_load_stackoverflow)
FR (1) FR2142583B1 (enrdf_load_stackoverflow)
GB (1) GB1310320A (enrdf_load_stackoverflow)
NL (1) NL7108226A (enrdf_load_stackoverflow)

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US3852207A (en) * 1973-03-26 1974-12-03 Chevron Res Production of stable lubricating oils by sequential hydrocracking and hydrogenation
US3915843A (en) * 1972-12-08 1975-10-28 Inst Francais Du Petrole Hydrocracking process and catalyst for producing multigrade oil of improved quality
US3962071A (en) * 1973-05-19 1976-06-08 Toa Nenryo Kogyo Kabushiki Kaisha Process for producing lubricating oils
US4263127A (en) * 1980-01-07 1981-04-21 Atlantic Richfield Company White oil process
US4515681A (en) * 1982-09-08 1985-05-07 Exxon Research & Engineering Co. Catalytic dewaxing using collapsed large pore zeolites
US4810355A (en) * 1985-12-12 1989-03-07 Amoco Corporation Process for preparing dehazed white oils
US4900707A (en) * 1987-12-18 1990-02-13 Exxon Research And Engineering Company Method for producing a wax isomerization catalyst
US4906601A (en) * 1988-12-16 1990-03-06 Exxon Research And Engineering Company Small particle low fluoride content catalyst
US4923588A (en) * 1988-12-16 1990-05-08 Exxon Research And Engineering Company Wax isomerization using small particle low fluoride content catalysts
US4937399A (en) * 1987-12-18 1990-06-26 Exxon Research And Engineering Company Method for isomerizing wax to lube base oils using a sized isomerization catalyst
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US5019662A (en) * 1988-05-19 1991-05-28 Uop Process for the production of white oil from heavy aromatic alkylate
US5057206A (en) * 1988-08-25 1991-10-15 Uop Process for the production of white oils
US5158671A (en) * 1987-12-18 1992-10-27 Exxon Research And Engineering Company Method for stabilizing hydroisomerates
US5320811A (en) * 1991-07-15 1994-06-14 The United States Of America As Represented By The Department Of Health And Human Services Thin layer chromatography direct sample application manifold
US5997732A (en) * 1997-12-22 1999-12-07 Chevron U.S.A. Inc. Clay treatment process for white mineral oil
WO2000029511A1 (en) * 1998-11-16 2000-05-25 Shell Internationale Research Maatschappij B.V. Catalytic dewaxing process
JP3062701B2 (ja) 1990-03-12 2000-07-12 アトランティック リッチフィールド カンパニー 食品級の品質のホワイト鉱油の製法
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US20070149723A1 (en) * 2005-12-23 2007-06-28 Goldschmidt Gmbh Silicone-containing graft copolymers based on styrene oxide-based silicone polyethers
US20090166251A1 (en) * 2007-12-28 2009-07-02 Hantzer Sylvain S All catalytic medicinal white oil production
US20150315493A1 (en) * 2013-11-06 2015-11-05 Axens Process for the production of white oils meeting the cfr standard from waste oils
CN107880932A (zh) * 2016-09-29 2018-04-06 中国石油化工股份有限公司 一种加氢催化剂级配方法和重油加氢处理方法

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US4474618A (en) * 1983-08-08 1984-10-02 Mobil Oil Corporation Overnight cloud and color in lube dewaxing using platinum zeolite catalyst
US5453176A (en) * 1993-10-13 1995-09-26 Narloch; Bruce A. Process for preparing white oil containing a high proportion of isoparaffins
US6051127A (en) * 1996-07-05 2000-04-18 Shell Oil Company Process for the preparation of lubricating base oils
CZ297084B6 (cs) * 1996-07-16 2006-09-13 Chevron U. S. A. Inc. Zpusob výroby zásob skladovatelných mazacích oleju

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US3340181A (en) * 1965-08-05 1967-09-05 Chevron Res Two-stage hydrotreatment for white oil manufacture
US3459656A (en) * 1966-08-16 1969-08-05 Sinclair Research Inc Making a white oil by two stages of catalytic hydrogenation
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US3915843A (en) * 1972-12-08 1975-10-28 Inst Francais Du Petrole Hydrocracking process and catalyst for producing multigrade oil of improved quality
US3852207A (en) * 1973-03-26 1974-12-03 Chevron Res Production of stable lubricating oils by sequential hydrocracking and hydrogenation
US3962071A (en) * 1973-05-19 1976-06-08 Toa Nenryo Kogyo Kabushiki Kaisha Process for producing lubricating oils
US4263127A (en) * 1980-01-07 1981-04-21 Atlantic Richfield Company White oil process
US4515681A (en) * 1982-09-08 1985-05-07 Exxon Research & Engineering Co. Catalytic dewaxing using collapsed large pore zeolites
US4810355A (en) * 1985-12-12 1989-03-07 Amoco Corporation Process for preparing dehazed white oils
US4900707A (en) * 1987-12-18 1990-02-13 Exxon Research And Engineering Company Method for producing a wax isomerization catalyst
US4937399A (en) * 1987-12-18 1990-06-26 Exxon Research And Engineering Company Method for isomerizing wax to lube base oils using a sized isomerization catalyst
US5158671A (en) * 1987-12-18 1992-10-27 Exxon Research And Engineering Company Method for stabilizing hydroisomerates
US5019662A (en) * 1988-05-19 1991-05-28 Uop Process for the production of white oil from heavy aromatic alkylate
US5057206A (en) * 1988-08-25 1991-10-15 Uop Process for the production of white oils
US4906601A (en) * 1988-12-16 1990-03-06 Exxon Research And Engineering Company Small particle low fluoride content catalyst
US4923588A (en) * 1988-12-16 1990-05-08 Exxon Research And Engineering Company Wax isomerization using small particle low fluoride content catalysts
US4992159A (en) * 1988-12-16 1991-02-12 Exxon Research And Engineering Company Upgrading waxy distillates and raffinates by the process of hydrotreating and hydroisomerization
JP3062701B2 (ja) 1990-03-12 2000-07-12 アトランティック リッチフィールド カンパニー 食品級の品質のホワイト鉱油の製法
US5320811A (en) * 1991-07-15 1994-06-14 The United States Of America As Represented By The Department Of Health And Human Services Thin layer chromatography direct sample application manifold
US6607568B2 (en) 1995-10-17 2003-08-19 Exxonmobil Research And Engineering Company Synthetic diesel fuel and process for its production (law3 1 1)
US6296757B1 (en) 1995-10-17 2001-10-02 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6669743B2 (en) 1997-02-07 2003-12-30 Exxonmobil Research And Engineering Company Synthetic jet fuel and process for its production (law724)
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US5997732A (en) * 1997-12-22 1999-12-07 Chevron U.S.A. Inc. Clay treatment process for white mineral oil
US6576120B1 (en) 1998-11-16 2003-06-10 Shell Oil Company Catalytic dewaxing process
WO2000029511A1 (en) * 1998-11-16 2000-05-25 Shell Internationale Research Maatschappij B.V. Catalytic dewaxing process
US20070149723A1 (en) * 2005-12-23 2007-06-28 Goldschmidt Gmbh Silicone-containing graft copolymers based on styrene oxide-based silicone polyethers
US7594991B2 (en) 2007-12-28 2009-09-29 Exxonmobil Research And Engineering Company All catalytic medicinal white oil production
US20090166251A1 (en) * 2007-12-28 2009-07-02 Hantzer Sylvain S All catalytic medicinal white oil production
US20150315493A1 (en) * 2013-11-06 2015-11-05 Axens Process for the production of white oils meeting the cfr standard from waste oils
US10174264B2 (en) * 2013-11-06 2019-01-08 Axens Process for the production of white oils from waste oils
CN107880932A (zh) * 2016-09-29 2018-04-06 中国石油化工股份有限公司 一种加氢催化剂级配方法和重油加氢处理方法
CN107880932B (zh) * 2016-09-29 2019-09-24 中国石油化工股份有限公司 一种加氢催化剂级配方法和重油加氢处理方法

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GB1310320A (en) 1973-03-21
NL7108226A (enrdf_load_stackoverflow) 1972-12-19
FR2142583B1 (enrdf_load_stackoverflow) 1975-07-11

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