EP0447092B1 - 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
EP0447092B1
EP0447092B1 EP91301780A EP91301780A EP0447092B1 EP 0447092 B1 EP0447092 B1 EP 0447092B1 EP 91301780 A EP91301780 A EP 91301780A EP 91301780 A EP91301780 A EP 91301780A EP 0447092 B1 EP0447092 B1 EP 0447092B1
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EP
European Patent Office
Prior art keywords
hydrogenation
range
product
food grade
white mineral
Prior art date
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Revoked
Application number
EP91301780A
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German (de)
English (en)
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EP0447092A1 (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
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Atlantic Richfield Co
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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
    • 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.
  • US-A-4325804 describes a process for the production of a food grade quality white mineral oil from a hydrocarbon feedstock by means of a series of hydroprocessing steps.
  • the process requires a hydrocracking step which has the disadvantage that it requires high energy consumption levels and converts much of the aromatic content of the feedstock into a product having a non-white oil boiling range.
  • a method for the production of food grade quality white mineral oil from a naphthenic feedstock without solvent extraction or acid treatment in a continuous process wherein the feedstock is subjected to a plurality of hydroprocessing steps in series characterised in that
  • the feedstock is first hydrogenated followed by a step of separating gaseous constituents produced during the hydrogenation reaction, followed by a second stage of hydrogenation, followed by separation of the gaseous constituents produced by this second stage of hydrogenation, followed by a third and less severe hydrogenation step to produce the desired food grade white mineral oil.
  • Fig. 1 illustrates a prior art method of preparing a food grade white mineral oil.
  • a napthenic distillate is extracted with a solvent such as a phenol or N-methyl pyrrolidine to produce a hydrocarbon oil containing only 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 product a satisfactory food grade white mineral oil in the effluent line 19.
  • the approach of this invention involves subjecting a naphthenic distillate illustratively 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 50 to 70 percent of the aromatic hydrocarbons to yield an aromatic carbon content of 7 - 10 percent by weight.
  • a naphthenic distillate illustratively containing a concentration of aromatic carbons in the range of 15 - 25 percent by weight
  • 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 288°C to 399°C (550 degrees Fahrenheit to 750 degrees Fahrenheit), preferably 343°C to 371°C (650 degrees Fahrenheit - 700 degrees Fahrenheit) with a partial pressure of hydrogen in the range of 8.2 - 13.7 MPa gauge (1200 - 2000 pounds per square inch gauge (PSIG)), preferably 10.3 - 12.4 MPa (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 17.3 - 20.7 MPa gauge (2500 - 3000 PSIG), preferably 19.0 - 20.7 MPa gauge (2750 - 3000 PSIG) and a temperature in the range of 302°C - 399°C (575 - 750 degrees Fahrenheit), preferably 329°C - 371°C (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.
  • These gaseous constituents include hydrogen sulfide and ammonia, inter alia.
  • 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 13.7 - 20.7 MPa gauge (2000 - 3000 PSIG), preferably 17.2 MPa - 20.7 MPa gauge (2500 - 3000 PSIG) and temperature of only 191°C to 316°C (375 degrees Fahrenheit to 600 degrees Fahrenheit), preferably 232°C - 288°C (450 degrees Fahrenheit - 550 degrees Fahrenheit).
  • a hydrogenation catalyst containing a metal component of Group VIIIA class such as platinum, palladium or Nickel
  • platinum in the form usually utilized in reforming reactions with hydrogen partial pressure in the range of 13.7 - 20.7 MPa gauge (2000 - 3000 PSIG), preferably 17.2 MPa - 20.7 MPa gauge (2500 - 3000 PSIG) and temperature of only 191°C to 316°C (375 degrees Fahrenheit to 600 degrees Fahrenheit), preferably
  • 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 hydrogenation 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 hydrogenation 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)

Claims (9)

  1. Procédé de préparation d'une huile minérale blanche de qualité alimentaire à partir d'un substrat naphténique sans extraction par un solvant et sans traitement avec un acide, en continu, dans lequel le substrat est soumis à une pluralité d'étapes d'hydrotraitement en série, caractérisé en ce que :
    (i) on soumet ledit substrat à trois opérations d'hydrogénation ;
    (ii) on effectue la première opération d'hydrogénation à une température comprise entre 288°C et 399°C (entre 550°F et 750°F) et à une pression partielle d'hydrogène d'au moins 8,2 MPa au manomètre (1200 psig), mais moins de 13,7 MPa au manomètre (2000 psig) ;
    (iii) le flux d'amenée à la deuxième opération comprend le produit liquide provenant de la première opération ; et
    (iv) le flux d'amenée à la troisième opération comprend le produit liquide provenant de la deuxième opération.
  2. Procédé tel que revendiqué dans la revendication 1, comprenant les étapes consistant à :
    (a) réduire la teneur en composés aromatiques du flux d'amenée d'environ 50 % lors d'une première opération d'hydrogénation ;
    (b) séparer les constituants gazeux du produit liquide hydrogéné de l'opération (a) ;
    (c) réduire la teneur en carbures aromatiques du produit liquide de l'opération (a), après avoir séparé les constituants gazeux de celui-ci, à environ 1 %, en soumettant ledit produit à une deuxième opération d'hydrogénation ;
    (d) séparer les constituants gazeux du produit d'hydrogénation de l'opération (c) ; et
    (e) produire l'huile minérale blanche de qualité alimentaire ne contenant qu'une trace de composés aromatiques, en soumettant le produit liquide de l'étape (c), après avoir séparé les constituants gazeux de celui-ci, à une opération d'hydrogénation finale dans des conditions moins rigoureuses que celles de l'opération (a) et de l'opération (b).
  3. Procédé tel que revendiqué dans la revendication 1 ou 2, dans lequel le flux d'amenée est un distillat naphténique ou cycloparaffinique contenant une concentration de carbures aromatiques valant de 15 à 25 % en poids.
  4. Procédé selon la revendication 3, dans lequel on effectue ladite première hydrogénation avec un catalyseur de nickel-molybdène, et lesdits constituants gazeux dudit produit hydrogéné comprennent du sulfure d'hydrogène et de l'ammoniac, que l'on sépare par rectification.
  5. Procédé selon la revendication 3 ou 4, dans lequel on effectue ladite première hydrogénation à une pression partielle d'hydrogène comprise entre 10,3 et 12,4 MPa (1500 - 1800 PSIG), et à une température comprise entre 343°C et 371°C (650 - 700°F).
  6. Procédé selon l'une quelconque des revendications 2 à 5, dans lequel on effectue ladite deuxième hydrogénation avec un catalyseur de nickel-molybdène, et lesdits constituants gazeux dudit deuxième produit hydrogéné comprennent du sulfure d'hydrogène et de l'ammoniac, que l'on sépare par rectification.
  7. Procédé selon la revendication 6, dans lequel ladite pression partielle d'hydrogène est comprise entre 19,0 et 20,7 MPa (2750 - 3000 PSIG), et où ladite température est comprise entre 329 et 371°C (625 - 700°F).
  8. Procédé selon l'une quelconque des revendications 2 à 7, dans lequel on effectue ladite hydrogénation finale moins rigoureuse en présence d'un catalyseur de reformation du platine.
  9. Procédé selon la revendication 8, dans lequel on effectue ladite hydrogénation finale moins rigoureuse à une pression partielle d'hydrogène comprise entre 17,2 et 20,7 MPa (2500 - 3000 PSIG) et à une température comprise entre 232 et 288°C (450 - 550°F).
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)

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

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ID=23952542

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EP91301780A Revoked EP0447092B1 (fr) 1990-03-12 1991-03-04 Méthode de préparation d'huile minérale blanche de qualité alimentaire

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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)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6635170B2 (en) * 2000-12-14 2003-10-21 Exxonmobil Research And Engineering Company Hydroprocessing process with integrated interstage stripping

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2398104A1 (fr) * 1977-07-20 1979-02-16 Shell France Huile lubrifiante stable a la lumiere
US4325804A (en) * 1980-11-17 1982-04-20 Atlantic Richfield Company Process for producing lubricating oils and white oils

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Hawley's Chemical Dictionary, 11th Edition, Van Nostrand Reinhold Company, (1987), page 616 *

Also Published As

Publication number Publication date
ATE109199T1 (de) 1994-08-15
BR9100974A (pt) 1991-11-05
HU208615B (en) 1993-12-28
DE69103049T2 (de) 1994-11-17
HU910783D0 (en) 1991-09-30
GR910300140T1 (en) 1992-06-30
DE69103049D1 (de) 1994-09-01
ES2025542T1 (es) 1992-04-01
EP0447092A1 (fr) 1991-09-18
CZ279524B6 (cs) 1995-05-17
CS64491A3 (en) 1992-03-18
HUT59573A (en) 1992-06-29
JPH04220492A (ja) 1992-08-11
DE447092T1 (de) 1992-02-27
JP3062701B2 (ja) 2000-07-12

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