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
  • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
  • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
  • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
  • C10G67/0409—Extraction of unsaturated hydrocarbons
  • C10G67/0418—The hydrotreatment being a hydrorefining
• • 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

Definitions

• the present invention is concerned generally with the production of process oils from paraffinic rich feeds.
• paraffinic rich feeds make them particularly useful in a broad range of oils used in a wide variety of industrial applications.
• the paraffinic oils may be used in rubber processing for reasons such as reducing the mixing temperature during the processing of the rubber, and preventing scorching or burning of the rubber polymer when it is being ground down to a powder, or modifying the physical properties of the finished rubber.
• These oils are finished by a refining procedure which imparts to the oils their excellent stability, low staining characteristics and consistent quality.
• one object of the present invention is to provide a process oil that has a lower a aniline point and consequently increased solvency above what could be obtained from paraffinic distillates alone, by using paraffinic distillates in admixture with their co-produced extracts.
• a method for producing a process oil which comprises:
• paraffinic rich feed used to produce process oils in accordance with the method of the present invention will comprise virgin and/or synthetic hydrocarbons, although other paraffinic rich materials obtained by extraction or alkane or ketone dewaxing, catalytic dewaxing and the like may be utilized.
• an aromatic extract oil is added to the paraffinic rich feed to provide a blended feed for hydrotreating.
• the aromatic extract oil used in the present invention will have an aniline point less than about 60°C for high viscosity oils (e.g., greater than about 35 cSt @ 100°C) and less than about 70°C for low viscosity oils (e.g., about 2 cSt to about 35 cSt @ 100°C).
• Such an aromatic oil suitable in the process of the present invention is readily obtained by extracting a naphthenic or paraffinic rich feed such as a distillate with aromatic extraction solvents at temperatures in the range of about 50°C to about 150°C in extraction units known in the art.
• Typical aromatic extraction solvents include N-methylpyrrolidone, phenol, N-N-dimethylformamide, dimethylsulfoxide, methylcarbonate, morpholine, furfural. and the like and preferably N-methylpyrrolidone or phenol.
• Solvent to oil treat ratios are generally about 0.5:1 to about 3:1.
• the extraction solvent preferably contains water in the range of about 1 vol.% to about 20 vol. %. Basically the extraction can be conducted in a counter-current type extraction unit.
• the resultant aromatic rich solvent extract stream is then solvent stripped to provide an aromatic extract oil having an aromatic content of about 50% to 90% by weight.
• the aromatic extract oil is mixed with the same or different viscosity paraffinic rich feed in an extract to feed volume ratio in the range of about 10:90 to about 90:10, preferably 25:75 to 50:50.
• Typical but not limiting examples of paraffinic feed and extract oils are provided in Tables 1 and 2 for low and high viscosity oils, respectively.
• the resultant mixture is then subjected to a solvent extraction using aromatic extraction solvents such as those previously described in connection with obtaining the aromatic extract oil for blending, but under generally milder conditions.
• aromatic extraction solvents such as those previously described in connection with obtaining the aromatic extract oil for blending, but under generally milder conditions.
• the ratio of solvent to blended feed is generally in the range of about 0.5:1 to about 3:1 and the extraction is conducted at a temperature in the range of about 50°C to about 150°C and the extraction solvent contains water in the range of about 1 vol% to about 20 vol%; and preferably greater than about 5 vol% to produce a raffinate.
• the resultant raffinate is then subjected to a hydrotreating step in a single hydrotreating stage which is maintained at a temperature in the range of about 275°C to about 375°C and preferably within the range of 340°C to 365°C at a hydrogen partial pressure in the range of about 300 to about 2500 psia and preferably from 500 to 1200 psia.
• Hydrotreating is conducted at a liquid hourly space velocity in the range from about 0. 1 to about 2.0 v/v/hour and preferably from 0.5 to 1.0 v/v/hour.
• the hydrotreating is effected conventionally under hydrogen pressure and with a conventional catalyst.
• Catalytic metals such as nickel, cobalt, tungsten, iron, molybdenum, manganese, platinum, palladium, and combinations of these supported on conventional supports such as alumina, silica, magnesia, and combinations of these with or without acid-acting substances such as halogens and phosphorous may be employed.
• a particularly preferred catalyst is a nickel molybdenum phosphorus catalyst supported on alumina, for example KF-840.
• An optional dewaxing step could be conducted on the paraffinic rich feed or the hydrofinished product using catalytic dewaxing or alkane or ketone or catalytic dewaxing.

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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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Citations (2)

• 2000
  • 2000-06-15 EP EP00112679A patent/EP1164181A1/de not_active Withdrawn

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