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
  • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
  • C10G49/007—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 in the presence of hydrogen from a special source or of a special composition or having been purified by a special treatment
• • 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

• This invention relates to a method for improving the properties of lubricating oils. More particularly, it is concerned with the production of lubricating oils of improved viscosity index by contacting a lubricating oil fraction with a hydrogenation catalyst in the presence of hydrogen containing a minor amount of carbon monoxide.
• a less severe type of hydrogenation is generally referred to as hydrotreating or hydrofining.
• the catalyst Ordinarily in this type of reaction the catalyst has little if any cracking activity but a significant amount of molecular rearrangement occurs although the principal purpose is to saturate aromatics and convert organically combined sulfur and nitrogen to hydrogen sulfide and ammonia. The reactions are usually sufficiently severe to produce some low boiling material.
• hydrofinishing The least severe of the hydrogenation reactions is usually called hydrofinishing and its general purpose is to effect a slight reduction in the sulfur and nitrogen content of the charge material and to remove color bodies from the oil. Ordinarily in hydrofinishing there is little change in the over-all boiling range of the lube oil fraction feed and accordingly the yields of lube oil from this hydrogen treatment is generally within the range of about 90-100 percent. Hydrofinishing also has substantially no effect on the viscosity index of the charge.
• lubricating oils of improved viscosity index are prepared by contacting a lubricating oil fraction with a halogen-free hydrogenation catalyst in the presence of hydrogen containing a minor amount of carbon monoxide.
• the lubricating oil fractions used in the process of and may comprise waxy distillates, deresined, decarbonized or deasphalted residual stocks, naphthene base oils, hydrocracked residuaand the like.
• the reaction conditions in the hydrogenation zone include temperatures between about 550 and 850F., a preferred range being 600-800F. Suitable pressures include a range of about 500-2,000 psig. total pressure preferably 800l,500 psig.
• the lube oil charge stock may be introduced into the reaction zone at a space velocity of between about 0.1 and 5.0 volumes of oil per volume of catalyst per hour, a preferred range being between 0.3 and 2.0 v/v/hr.
• Hydrogen may be introduced into the reaction zone at a rate between about 500 and 10,000 standard cubic feet per barrel of charge, a preferred range being from 1,000 to 7,500 scfb.
• the hydrogen need not be pure. Satisfactory results may be obtained using hydrogen having a purity as low as 65 per cent.
• Suitable sources of hydrogen are catalytic reformer by-product hydrogen, electrolytic hydrogen and hydrogen produced by the partial oxidation of a hydrocarbonaceous material followed by shift conversion and CO removal.
• the carbon monoxide may be introduced into the hydrogenation zone at a rate between about 0.01 and 10.0 mol per cent of the pressuring gas which is referred to herein as hydrogen.
• a preferred range is between 0.1 and 1.0 mol percent.
• the hydrogen and carbon monoxide are introducedas a mixture.
• the catalysts used in the process of our invention are composed of a hydrogenating component on a support.
• Suitable hydrogenating components comprise Group VIII metals such as the noble metals, e.g., platinum or palladium or iron group metals, e.g., cobalt and nickel and the compounds thereof.
• a' Group VI metal such as molybdenum or tungsten or compounds thereof.
• thehydrogenating component is an iron group metal it may be present in an amount between about 1 and 10 percent by weight of the catalyst composite preferably between 2 and 8 percent.
• the Group VI metal used in conjunction with the Group VIII metal may suitably amount to between about 5 and 35 percent by weight of the composite, a preferred range being between 8 and 25 percent.
• the hydrogenating components may be present as the metal or metal oxide or sulfide.
• Suitable catalyst supports comprise refractory inorganic amorphous oxides such as alumina, silica, magnesia, zirconia, titania and the like and mixtures thereof.
• the catalyst support comprises a mixture of The following examples are given for illustrative purposes only.
• the charge is a dewaxed paraffin distillites are those obtained by the removal of alkali metal 10 late having kinematic viscosity at 1 f 7 5 ions from naturally Occurring or synthetic Zeolites centistokes and at 2 lOF. 12.10 centistokes.
• the vislng P openings of 6-13A u as faulasite and cosity index of the charge is 49.
• the charge is hydrolite Y and the like.
• the zeolite will have an cracked by being passed over a catalyst containing 3.5 alkali metal content of less than about 2.0 wt. percent. percent nickel and 18.5 percent molybdenum on alu-
• the catalyst should also be free of halogen. mina.
• the catalyst in particulate form, may be used as a 750F. and three at a temperature of 825F., one run slurry, a moving bed or a fixed bed.
• the reacat each temperature being free from carbon monoxide, tion is carried out by passing the reactants through a one using hydrogen containing 0.5 mol percent CO and fixed bed of catalyst pellets.
• Reactant flow may be upone using hydrogen containing 5.0 mol percent CO. ward or downward through the bed or the gasmay flow
• Data on the reaction conditions and product appear upwardly in countercurrent relationship to downwardly 7 below in Table l.
• Runs 1 and 2 show the activing in view of the. prior art which indicated that in e ity of the catalyst under standard CO-free operating hydroc'racking 0f gas oils and the like, the activity of conditions, In Runs 3 and 4 the hydrogen contained Q5 halogen-containing catalysts was suppressed and the mol percent CO. Runs 5 and 6 in which CO-free hydroactivity of halogen-free catalysts was not affected by gen was used show the residual effect of CO. in both the presence of CO.
• a process for moderating the hydrocracking of a lubricating oil fraction which comprises contacting said sure between about 500 and 5,000 psig, a space velocin its absence since the magnitude of viscosity decrease ity between about 0.1 and 5.0 v/v/hr. and a hydrogen is ordinarily taken as a measure of the extent of crackrateof between about 500 and 10,000 SCFB with a ing. Since it would be expected in view of the discushalogen-free hydrogenation catalyst in the presence of sion above that less cracking would occur in the presb t about 1 d 10 per-cent Carbon mono)- ence of carbon monoxide, it would be expected that the id ba ed on the hydrogen.
• EXAMPLE 111 4. The process of claim 2 in which the Group v111 This example shows the effect of the use of carbon meta] ls mckel' monoxide during the mild hydrogenation of a hydro- T Process of Clam 2 Whch the Group Vm cracked deasphalted residuum using 0.5 wt. percent metal Cobalt palladium on a low sodium zeolite Y containing sup- 6.
• the support comprises a crystalline zeolite having uniform pore openings of between 6 and 13 A and an alkali metal content of less than 4.0 wt. percent.

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)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Lubricants (AREA)
• Catalysts (AREA)

Priority Applications (8)

Applications Claiming Priority (1)

Publications (1)

Family

ID=23392583

Family Applications (1)

Country Status (8)

Cited By (7)

• 1973
  • 1973-04-25 US US00354276A patent/US3803028A/en not_active Expired - Lifetime
• 1974
  • 1974-01-18 JP JP794574A patent/JPS5419881B2/ja not_active Expired
  • 1974-02-06 GB GB556174A patent/GB1463116A/en not_active Expired
  • 1974-02-28 FR FR7406790A patent/FR2227316A1/fr not_active Withdrawn
  • 1974-03-26 CA CA195,996A patent/CA1024921A/en not_active Expired
  • 1974-03-28 DE DE2415022A patent/DE2415022A1/de active Pending
  • 1974-04-23 ES ES425590A patent/ES425590A1/es not_active Expired
  • 1974-04-23 IT IT21787/74A patent/IT1010003B/it active

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