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
  • C10G67/0445—The hydrotreatment being a hydrocracking
• • 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

• Lube oils of improved ultraviolet stability, color and viscosity index are obtained by hydrocracking a lube oil fraction and subjecting the product to solvent refining the then dewaxing.
• the preferred solvent is N-methyl-Z- pyrrolidone.
• the feed may be a wax distillate, a deasphalted residuum and may be subjected to pre-hydrocracking solvent refining step.
• distillation is employed as a means of separating a crude oil into fractions of various viscosities
• solvent refining with, for example, furfural, sulfur dioxide or phenol is ordinarily used as a means of removing aromatic compounds and thereby improving the viscosity index
• solvent dewaxing using for example a mixture of methyl ethyl ketone and toluene is a used to improve low temperature properties by lowering th pour point of the oil and clay contacting is used generally as a final step to further improve the color and to neutralize the oil after acid treating.
• a crude oil is topped under atmospheric pressure to produce light distillates and an atmospheric reduced crude which is then vacuum distilled to produce lube oil distillates and the residue from the vacuum distillation is deasphalted to yield residual lubricating stocks.
• the various lube oil fractions are then further processed by solvent refining, dewaxing, acid treating and clay contacting.
• the solvent extraction step is carried out first to recover about 4590% of the charge as solvent refined oil and to reject about 10-55% of the charge as dark colored viscous extract. Since the extract amounts to a relatively high percentage of the charge and is not suitable for up-grading by dewaxing and clay contacting to a satisfactory quality level for use as a lube oil, solvent extraction has, up to the present been the most logical and economical step to apply first.
• the solvent refined oil is contacted 'with clay Patented May 2, 1972 to improve its color and then dewaxed alhtough in some instances it may be desirable to dewax prior to clay contacting.
• Another object is to improve the color of a hydrocracked lube oil. Still another object is to increase the viscosity index of a hydrocracked lube oil.
• a lubricating oil which has been derived from a hydrocracking process is subject to solvent refining and if desired the solvent refined product is dewaxed to lower the pour point.
• the process of the invention may be applied to a variety of feedstocks.
• the feed may be obtained by subjecting a vacuum residuum to deasphalting with a low molecular weight hydrocarbon such as propane or butane.
• the deasphalted residuum can then be hydrocracked and solvent refined. It is also possible to feed a wax distillate to the hydrocracking stage.
• the feed whether obtained by vacuum distillation or by deasphalting a vacuum residuum may be subjected to a preliminary solvent refining before being subjected to hydrocracking.
• a lubricating oil fraction which has been obtained from a residuum such as atmospheric residuum or vacuum residuum by a simultaneous deasphalting-solvent refining procedure in which the residuum is treated not with the conventional low molecular weight hydrocarbon deasphalting agents but with a solvent such as furfural or N-methyl-2-pyrrolidone and the raffinate of reduced aromatic and asphalt content is charged to the hydrocracking zone.
• the reaction conditions for the hydrocracking may be varied depending on the amount of hydrocracking desired and on the charge stock.
• Typical reaction conditions include a temperature of about 700-900 F., preferably 750-850 F.
• the pressure may range between about 500 and 5000 p.s.i.g., a preferred range being from 1000 to 2500 p.s.i.g.
• Space velocities may vary between about 0.1 and 10.0 v./v./hr. with a preferred range being 0.3-4.5.
• Hydrogen rates of from 100010,000 s.c.f.b. have been found satisfactory although rates of 3000-10,000 s.c.f.b are preferred.
• Hydrogen from any suitable source such as electrolytic hydrogen, hydrogen obtained from the partial combustion of hydrocarbonaceous material followed by shift conversion and purification or catalytic reformer by-product hydrogen may be used.
• the hydrogen should have a purity of between about and 100% with hydrogen purities of 95 volume percent being preferred.
• the oil and hydrogen are brought into contact in the presence of a catalyst.
• the catalyst may be in the form of a fixed bed, a moving bed, a fluidized bed or may be slurried with the oil.
• Hydrogen flow may be upward or downward through the reactor as may be the flow of the oil.
• both the oil and a portion of the hydrogen are introduced at the top of a reactor containing a fixed bed of the catalyst, the balance of the hydrogen being introduced at intermediate points in the reactor for cooling purposes.
• the catalyst for the hydrocracking step preferably comprises a compound of a Grorp VI metal such as molybdenum, chromium or tungsten or a compound of a Group VIII metal such as cobalt, iron or nickel and mixtures thereof.
• a Grorp VI metal such as molybdenum, chromium or tungsten
• a Group VIII metal such as cobalt, iron or nickel and mixtures thereof.
• the catalyst is charged to the reactor in oxide form although it can be expected that some reduction and some sulfidation take place during the course of the process so that after being on stream for some time the catalyst is probably a mixture of the metal, the metal sulfide and perhaps the oxide.
• the catalyst after being charged to the reactor but prior to the institution of the on stream period may be converted at least in part to the sulfide form for example by contact with a gas such as a mixture of hydrogen and a sulfiding agent, e.g. hydrogen sulfide, methyl mercaptan or carbon disulfide.
• a gas such as a mixture of hydrogen and a sulfiding agent, e.g. hydrogen sulfide, methyl mercaptan or carbon disulfide.
• the Group VIII metal may be present in an amount varying from 1 to 20% by weight of the total catalyst composite, preferably 2-15% and the Group VI metal may be present in an amount ranging from about 5-40%, preferably 7-25
• the metal components are supported on a refractory inorganic oxide such as decationized zeolite, alumina, zirconia, silica or magnesia and mixtures thereof optionally promoted with an acidic material such as boron oxide or a halogen.
• the catalyst has a surface area of at least 150 m. /g., and a pore volume of at least 0.5 cc./ g.
• the upper limit of the surface area and pore volume is governed by the hardness and ruggedness of the catalyst.
• the surface area probably should not exceed about 800 mP/g. and the pore volume should not exceed about 0.8 cc./ g.
• the catalyst may be prepared by any of the methods well known in the art, such as by impregnating the support with a solution of a salt of one of the metals, filtering, drying and then if desired impregnating with a solution of a salt of another metal, filtering, drying and calcining in a manner well known in the art.
• the eflluent from the hydrocracker is cooled and hydrogen-rich gas separated therefrom and recycled to the hydrocracking zone.
• the hydrogen-rich stream is scrubbed with water to remove any ammonia contained therein or a portion thereof may be bled from the system to prevent the buildup of ammonia and/ or low molecular weight hydrocarbons.
• Hydrogen is added to the recycle stream to replace that consumed in the hydrocracking reaction and if necessary to replace any hydrogen purged from the system.
• Lubricating oil fractions are recovered from the balance of the hydrocracker efiluent by distillation, if necessary, at reduced pressure.
• solvent refining step The hydrocracked oil is then subjected to a solvent refining step.
• Suitable solvents are furfural, nitrobenzene, dimethyl formamide, liquid S0 and the like. However, because of its chemical stability, the improved ultraviolet stability of the product and its superior solvent capacity, N-methyl-Z-pyrrolidone is the preferred solvent.
• Solvents are generally used at dosages of 100-600%, at temperatures between l20-250 F., preferred conditions being dosages of 100-300% and temperatures between 120 and 180 F.
• the unusual feature of this invention is that solvent refining prior to hydrocracking alone is not sufiicient to render the oil stable to ultraviolet light but a solvent refining after hydrocracking particularly when the solvent is N-methyl-Z-pyrrolidone, results in an improved oil.
• solvent refining conditions for the second solvent refining need not be as severe as those for the first although in commercial installations it may be advantageous to use the same conditions.
• the oil may be subjected to dewaxing to reduce its pour point.
• the rafiinate from the solvent refining is passed into contact with a catalyst c0mprising a hydrogenating component, such as is used in the hydrocracking catalyst, supported on a decationized mordenite.
• the support is made by treating a synthetic mordenite with acid to replace the sodium ions with hydrogen ions.
• the synthetic mordenite is treated with acid to the extent that a portion of the alumina is leached out to produce a mordenite having a silica:alumina mol ratio of at least 20 and having increased dewaxing activity.
• the catalytic dewaxing may be carried out at a temperature of at least 450 F., a pressure of at least p.s.i.g., a space velocity of 0.2-5.0 v./v./hr. and a hydrogen rate of 1000-10,000 s.c.f.b.
• Preferred conditions in the catalytic dewaxing zone are a temperature of 450-800 F.., a pressure of 100-1500 p.s.i.g. and a space velocity of 0.2-2.0.
• the oil may be contacted with a dewaxing agent such as a mixture containing 40-60 volume percent of a ketone such as acetone, methyl ethyl ketone or normal butyl ketone and 60-40 volume percent of an aromatic compound such as benzene or toluene in a ratio of about 3-4 parts by volume of solvent per volume of oil, the mixture cooled to a temperature of about 0 to 20 F. and the waxy components removed by filtering or centrifuging. The filtrate is then subjected to flash distillation and stripping to remove the solvent.
• the resulting product is a lubricating oil of high viscosity index and good stability towards ultraviolet light.
• Table 1 column 1 shows the characteristics of the hydrocracked oil, column 2, the dewaxed hydrocracked oil, column 3 the characteristics of an oil obtained by refining the hydrocracked oil with N-methyl- 2-pyrrolidone at 180 F. and a dosage of 300% and column 4 the oil of column 3 after dewaxing.
• the dewaxing solvent is a mixture of equal parts by volume of toluene and methyl ethyl ketone.
• This example shows that the fioc formation of the hydrocracked oil in ultraviolet light is reduced by the mild solvent refining treatment. Additionally the viscosity index of the oil is improved 12 VI units. It also shows that solvent refining only prior to hydrocracking does not yield an oil stable to ultraviolet light but does show that when the solvent refining follows the hydrocracking the product oil shows the desired stability.
• Example II shows the superiority of N-methyl-Z-pyrrolidone over furfuralfor producing a product having stability towards ultraviolet light. It also shows that the hydrocracked oil which has not been treated with a solvent having an affinity for aromatics has very poor U.V. stability. In addition to improved ultraviolet stability, the solvent refining of the hydrocracked oil results in an oil with improved viscosity index.
• EXAMPLE III The hydrocracked deasphalted vacuum residuum used in Example II is solvent refined with N-methyl-Z-pyrrolidone on a mixer-settler countercurrent extractor with 176 vol. percent solvent dosage, 209 F. extraction temperature and a refined oil yield of 79 vol. percent.
• the properties of the dewaxed charge and dewaxed refined oil are shown in columns 1 and 2 respectively of Table III. The improvement in ultraviolet stability and viscosity index are again evident.
• the vacuum residuum obtained from a sweet Louisiana crude is treated with butane as a deasphalting agent and the deasphalted residuum is hydro cracked as in Example II.
• Solvent refining of the hydrocracked oil is conducted on a 12 stage mixer-settler countercurrent extractor using 105 -vol. percent N-methyl- 2-pyrrolidone at 120 F. extraction temperature. The refined oil is produced in 82 vol. percent yield. Properties of the hydrocracked oil before and after solvent refining are shown in columns 1 and 2 respectively of Table IV.
• a process for the production of a lubricating oil of improved viscosity index and ultraviolet stability which comprises contacting a lubricating oil fraction wth a hydrocracking catalyst comprising a Group VI metal and a Group VIII metal or compounds thereof on a support consisting essentially of alumina having a surface area between m. /g. and 800 m. /g. and a pore volume between 0.5 and 0.8 cc./g. under hydrocracking conditions including a temperature between 750 and 850 F. and extracting the hydrocracked oil with N- methyl 2 pyrrolidone to produce a lubricating oil rafiinate of improved viscosity index and ultraviolet stability.

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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)
• Lubricants (AREA)

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Cited By (12)

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• 1969
  • 1969-11-12 US US876113A patent/US3660273A/en not_active Expired - Lifetime
• 1970
  • 1970-11-07 DE DE2054940A patent/DE2054940C3/de not_active Expired
  • 1970-11-11 JP JP45098814A patent/JPS4923571B1/ja active Pending
  • 1970-11-12 NL NL7016619A patent/NL7016619A/xx unknown
  • 1970-11-12 CA CA098021A patent/CA931094A/en not_active Expired
  • 1970-11-12 ES ES385469A patent/ES385469A1/es not_active Expired
  • 1970-11-13 FR FR7040656A patent/FR2073344B2/fr not_active Expired

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