EP0447092A1 - Méthode de préparation d'huile minérale blanche de qualité alimentaire - Google Patents

Méthode de préparation d'huile minérale blanche de qualité alimentaire Download PDF

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Publication number
EP0447092A1
EP0447092A1 EP91301780A EP91301780A EP0447092A1 EP 0447092 A1 EP0447092 A1 EP 0447092A1 EP 91301780 A EP91301780 A EP 91301780A EP 91301780 A EP91301780 A EP 91301780A EP 0447092 A1 EP0447092 A1 EP 0447092A1
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EP
European Patent Office
Prior art keywords
hydrogenation
food grade
mineral oil
white mineral
product
Prior art date
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Granted
Application number
EP91301780A
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German (de)
English (en)
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EP0447092B1 (fr
Inventor
Gary L. Everett
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.)
Atlantic Richfield Co
Original Assignee
Atlantic Richfield Co
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Filing date
Publication date
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Application filed by Atlantic Richfield Co filed Critical Atlantic Richfield Co
Publication of EP0447092A1 publication Critical patent/EP0447092A1/fr
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Anticipated expiration legal-status Critical
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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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
    • 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 the method of producing food grade quality white mineral oil. More particularly, this invention relates to a method of producing from a naphthenic distillate as a feedstock, a food grade white mineral oil with only a trace of aromatics therewithin.
  • the prior art has failed to provide an economical method of achieving a food grade quality white mineral oil without expensive and labor intensive steps such as acid treating, neutralization and adsorbing of undesired constituents from the product.
  • a method of producing a food grade quality of white mineral oil by subjecting a naphthenic or cycloparaffinic feedstock to three stages of hydroprocessing without any solvent extraction or acid treatment prior to the treatment to give the final desired quality with only a trace of the aromatic hydrocarbons, or aromatic carbons, therewithin.
  • a method of producing a food grade quality in which a naphthenic feedstock is first hydrogenated followed by a step of separating gaseous constituents produced during the hydrogenation reactions, followed by a second stage of hydroprocessing, or hydrogenation, followed by separation of the gaseous constituents produced by this second stage of hydrogenation, followed by a third and less severe hydrotreating step to produce the desired food grade white mineral oil.
  • Fig. 1 is a schematic flow diagram of a prior art process for producing food grade white mineral oil.
  • Fig. 2 is a schematic flow diagram of the process of this invention for producing food grade white mineral oil.
  • Fig. 1 illustrates a prior art method of preparing a food grade white mineral oil.
  • a naphthenic distillate is extracted with a solvent such as a phenol or N-methyl pyrrolidine to produce a hydrocarbon oil containing only about 4 to 7 percent aromatic carbons which is subjected to an acid treatment.
  • the bottoms fraction recovered from the acid treatment then emerges as acid sludge whereas from the first step of solvent extraction, a solvent extract containing a high level of aromatic compounds is recovered as a bottom product.
  • a finishing step consisting of an adsorption tower 17 employing clay or a hydrotreater tower 17 using hydrogen is employed to lower the remaining trace quantity of aromatics and produce a satisfactory food grade white mineral oil in the effluent line 19.
  • the approach of this invention involves subjecting a naphthenic distillate containing a concentration of aromatic carbons in the range of 15 - 25 percent by weight to hydrogenation to produce a hydrogenated product in which there is a reduction of about 50 to 70 percent of the aromatic hydrocarbons to yield an aromatic carbon content of 7 - 10 percent by weight.
  • a naphthenic distillate containing a concentration of aromatic carbons in the range of 15 - 25 percent by weight to hydrogenation to produce a hydrogenated product in which there is a reduction of about 50 to 70 percent of the aromatic hydrocarbons to yield an aromatic carbon content of 7 - 10 percent by weight.
  • Fig. 2 at stage 1, also labeled tower 21.
  • the term "naphthenic distillates” is synonymous with cycloparaffinic distillates. Normally these distillates contain about 15 - 25 percent by weight of aromatic carbons.
  • These naphthenic distillates come in via line 23, Fig. 2. Hydrogen is fed through line 25 in Fig. 2.
  • Both feed constituents are admixed prior to entering stage 1 where hydrogenation is carried out in the presence of a hydrogenation catalyst containing metal components from the Group VIIIA class, preferably Nickel and from the Group VIA class, preferably Molybdenum at a temperature of 550 degrees Fahrenheit to 750 degrees Fahrenheit, preferably about 650 degrees Fahrenheit - 700 degrees Fahrenheit with a partial pressure of hydrogen in the range of 1200 - 2000 pounds per square inch gauge (PSIG), preferably about 1500 - 1800 pounds per square inch gauge.
  • PSIG pounds per square inch gauge
  • the gaseous constituents of the hydrogenated product in line 27 are separated from liquid constituents and flow out through the overhead line 29.
  • the overhead line 29 carries from the stripper 31 hydrogen sulfide and ammonia, inter alia, as the gaseous products of the hydrogenation reactions carried out in the hydrogenation tower of stage 1, labelled 21.
  • the aromatic carbon content of the liquid constituents will have been reduced to about 7 - 10 percent aromatic carbons as in the liquid bottom draw from the stripper, line 33.
  • These liquid bottoms containing only about half as much aromatic carbons as the initial feedstock in line 23, or less, are then sent through line 35 to a second hydrogenation tower 37.
  • the liquid bottoms, or hydrogenated product from the first stage, in line 35 is admixed with hydrogen by way of line 39.
  • a second hydrogenation is carried out at rather severe conditions in the presence of a hydrogenation catalyst containing metal components from the Group VIIIA class, preferably Nickel and from the Group VIA class, preferably Molybdenum, with the hydrogen partial pressure in the range of 2500 - 3000 PSIG, preferably 2750 - 3000 PSIG and a temperature in the range of 575 - 750 degrees Fahrenheit, preferably 625 - 700 degrees Fahrenheit.
  • the entire reactor effluent then exits by a line 41 to stripper 43 and again the gaseous constituents of the second hydrogenation stage reaction product are separated from liquid constituents and exit line 45 from the second stripper 47.
  • the resulting liquid bottoms from the stripper 43, in line 49, contain only about 1 percent of aromatic carbons and they are sent, as by line 51 to be admixed with hydrogen in line 53 and the hydrogenation as a final step is carried out in stage 3, or the final, less severe hydrogenation of stage 3 in the hydrogenation tower 55.
  • a hydrogenation catalyst containing a metal component of Group VIIIA class such as platinum, palladium or Nickel, preferably platinum in the form usually utilized in reforming reactions with hydrogen partial pressure in the range of 2000 - 3000 PSIG, preferably 2500 - 3000 PSIG and temperature of only about 375 degrees Fahrenheit to 600 degrees Fahrenheit, preferably 450 degrees Fahrenheit - 550 degrees Fahrenheit.
  • the liquid bottoms draw in the line 57 will have only about 0.3 percent or less by weight of aromatic constituents and this trace of aromatics is satisfactory as a food grade white mineral oil.
  • the polynucular aromatics will comprise less than 30 parts per million (PPM) of the final food grade white mineral oil.
  • the naphthenic distillate comprising the initial feedstock is fed into and admixed with the hydrogen at the desired partial pressure in the incoming stream and hydrogenation is carried out in stage 1.
  • the gaseous constituents are allowed to separate from the liquid constituents such that the gases pass out the overhead stream in line 29 and the bottoms pass out the liquid stream 33 and are then fed through the line 35, Fig. 2, to the second stage, or hydrotreating tower, 37.
  • the admixture of hydrogen at its high partial pressure with the liquid constituents effects a direct reaction at elevated temperatures over suitable catalyst to produce the reduction in the aromatic carbons in line 41 such that after the gaseous constituents are separated and go to the overhead line 45, the liquid bottom draw 49 can be fed, low as it is in aromatic carbons, to the third hydrogenation stage 55.
  • the third hydrogenation stage 55 At the entrance to the third stage, it is admixed with high pressure hydrogen at the desired high partial pressure and the hydrogenation reactions carried out in the third hydrotreating tower 55. The result is that the final product comes out the bottom effluent line 57.
  • the desired food grade quality white mineral oil is produced in the line 57 by a process that differs substantially from the prior art technology for preparing food grade white mineral oil.

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)
  • Edible Oils And Fats (AREA)
  • Fats And Perfumes (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)
  • Lubricants (AREA)
  • Non-Alcoholic Beverages (AREA)
EP91301780A 1990-03-12 1991-03-04 Méthode de préparation d'huile minérale blanche de qualité alimentaire Revoked EP0447092B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US49151190A 1990-03-12 1990-03-12
US491511 1990-03-12

Publications (2)

Publication Number Publication Date
EP0447092A1 true EP0447092A1 (fr) 1991-09-18
EP0447092B1 EP0447092B1 (fr) 1994-07-27

Family

ID=23952542

Family Applications (1)

Application Number Title Priority Date Filing Date
EP91301780A Revoked EP0447092B1 (fr) 1990-03-12 1991-03-04 Méthode de préparation d'huile minérale blanche de qualité alimentaire

Country Status (9)

Country Link
EP (1) EP0447092B1 (fr)
JP (1) JP3062701B2 (fr)
AT (1) ATE109199T1 (fr)
BR (1) BR9100974A (fr)
CZ (1) CZ279524B6 (fr)
DE (2) DE69103049T2 (fr)
ES (1) ES2025542T1 (fr)
GR (1) GR910300140T1 (fr)
HU (1) HU208615B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1352039A4 (fr) * 2000-12-14 2005-03-16 Exxonmobil Res & Eng Co Procede d'hydrotraitement comprenant un degazolinage intermediaire

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2001339A (en) * 1977-07-20 1979-01-31 Shell Int Research Process for the preparation of a light-stable lubricating oil
US4325804A (en) * 1980-11-17 1982-04-20 Atlantic Richfield Company Process for producing lubricating oils and white oils

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3629096A (en) 1967-06-21 1971-12-21 Atlantic Richfield Co Production of technical white mineral oil

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2001339A (en) * 1977-07-20 1979-01-31 Shell Int Research Process for the preparation of a light-stable lubricating oil
US4325804A (en) * 1980-11-17 1982-04-20 Atlantic Richfield Company Process for producing lubricating oils and white oils

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1352039A4 (fr) * 2000-12-14 2005-03-16 Exxonmobil Res & Eng Co Procede d'hydrotraitement comprenant un degazolinage intermediaire

Also Published As

Publication number Publication date
DE447092T1 (de) 1992-02-27
DE69103049D1 (de) 1994-09-01
HU910783D0 (en) 1991-09-30
JPH04220492A (ja) 1992-08-11
DE69103049T2 (de) 1994-11-17
GR910300140T1 (en) 1992-06-30
CZ279524B6 (cs) 1995-05-17
BR9100974A (pt) 1991-11-05
ATE109199T1 (de) 1994-08-15
JP3062701B2 (ja) 2000-07-12
EP0447092B1 (fr) 1994-07-27
HU208615B (en) 1993-12-28
ES2025542T1 (es) 1992-04-01
HUT59573A (en) 1992-06-29
CS64491A3 (en) 1992-03-18

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