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
• • 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.
• process oils are used in a wide variety of industrial applications. For example, they are used in processing natural and synthetic rubbers for a number of reasons such as reducing the mixing temperature during 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 and the like.
• one object of the present invention is to provide a process oil that has a lower aniline point and consequently increased solvency above what could be obtained from paraffinic distillates alone, by using paraffinic distillates in admixture with their coproduced extracts.
• a method for producing a process oil comprises adding an aromatic containing extract oil to a paraffinic rich feed to provide a blended feed for processing; hydrotreating the feed in a first hydrotreating stage maintained at a temperature of about 300°C to about 375°C and a hydrogen partial pressure of about 300 to about 2500 psia to convert at least a portion of the sulfur in the feed to hydrogen sulfide and nitrogen in the feed to ammonia; stripping the hydrotreated feed from the first hydrotreating stage to remove hydrogen sulfide and ammonia; thereafter hydrotreating the hydrotreated feed in a second hydrotreating stage maintained at a temperature lower than the first stage in the range of about 275°C to about 370°C and a hydrogen pressure of about 300 to about 2500 psia to form a process oil.
• 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 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 dimethyl formamide, dimethylsulfoxide, methylcarbonate, morpholine, furfural and the like, preferably N-methylpyrrolidone or phenol.
• Solvent to oil treat ratios are generally from about 0.5:1 to about 3:1.
• the extraction solvent preferably contains water in the range from 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 in the range 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 and extract oils are provided in Tables 1 and 2 for low viscosity and high viscosity oils, respectively.
• the resultant mixture is then subjected to hydrotreating in a first hydrotreating stage.
• the first hydrotreating stage preferably is maintained within the range of about 300°C to 375°C and more preferably within the range of about 340° to 365°C at a hydrogen partial pressure in the range from about 300 to about 2500 psia and preferably from 500 to 1200 psia.
• Hydrotreating is conducted in the first stage 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, sufficient to convert at least a portion of the sulfur present in the feed to hydrogen sulfide and nitrogen in the feed to ammonia.
• the hydrotreated feed from the first hydrotreating stage then is passed into an intermediate stripping stage, for example, to remove the hydrogen sulfide and ammonia.
• the hydrotreated feed from the intermediate stripping stage is treated in a second hydrotreating stage which is maintained at a temperature in the range of about 275°C to about 370°C and preferably in the range of about 300°C to about 330°C at a hydrogen partial pressure of about 300 to about 2500 psia and preferably in the range of 500 to 1200 psia and at a space velocity of about 0.1 to about 2.0 v/v/hour, for a time sufficient to produce a process oil, for example, having an aniline point below about 65°C for a low viscosity oil and below about 100°C for a high viscosity oil.
• 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 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 (5)

• 2000
  • 2000-01-19 EP EP00100275A patent/EP1118652A1/fr not_active Withdrawn

Patent Citations (5)

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