USRE30529E - Manufacture of naphthenic type lubricating oils - Google Patents
Manufacture of naphthenic type lubricating oils Download PDFInfo
- Publication number
- USRE30529E USRE30529E US06/078,616 US7861679A USRE30529E US RE30529 E USRE30529 E US RE30529E US 7861679 A US7861679 A US 7861679A US RE30529 E USRE30529 E US RE30529E
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- US
- United States
- Prior art keywords
- low
- crude
- gas oil
- naphthenic type
- psig
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 title description 5
- 239000003921 oil Substances 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 14
- 229910052680 mordenite Inorganic materials 0.000 claims abstract description 11
- 238000005292 vacuum distillation Methods 0.000 claims abstract description 7
- 239000002184 metal Substances 0.000 claims abstract description 4
- 229910052751 metal Inorganic materials 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- 239000002904 solvent Substances 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000011593 sulfur Substances 0.000 claims description 7
- 229910052717 sulfur Inorganic materials 0.000 claims description 7
- 230000003197 catalytic effect Effects 0.000 claims description 5
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 3
- 229910052753 mercury Inorganic materials 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000003518 caustics Substances 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910003556 H2 SO4 Inorganic materials 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- XZMCDFZZKTWFGF-UHFFFAOYSA-N Cyanamide Chemical compound NC#N XZMCDFZZKTWFGF-UHFFFAOYSA-N 0.000 description 1
- 229910003296 Ni-Mo Inorganic materials 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
- B01J29/26—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
- B01J29/20—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type containing iron group metals, noble metals or copper
-
- 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
- Naphthenic lubricating oils are conventionally made from grade A or coastal, wax-free crudes by simple distillation of the crude in the presence of caustic. Due to such simple processing they have been relatively inexpensive.
- Naphthenic oils have naturally low pour points of from -50° F. in low viscosity grades to +20° F. in high viscosity grades. Their viscosity Index (VI) is poor, but, in many applications, this quality is secondary to cost considerations. There are also some applications where the particular properties of naphthenic lubes (very low pour point and relatively high content of aromatic compounds) make them desirable in spite of any price advantage.
- VI viscosity Index
- Solvent lubricating oils are made from waxy crudes. They require a complicated refining scheme and are, therefore, more expensive. VI is high and pour points of finished oils (after dewaxing) run 0 to +10° F. These lubes must be manufactured from selected waxy crudes, i.e., those with VI high enough to give at least 90-95 VI levels in the finished oils. Waxy crudes with lower VI potential are rejected for solvent lube manufacture and utilized only for fuels.
- This invention is directed to a process for manufacturing relatively inexpensive naphthenic type lubes from the low VI waxy crudes unsuitable for solvent lubes and now used for gasoline and fuels. Such a process is desirable because reserves of grade A or coastal crudes are seriously declining and no new fields of these grades have been discovered. Thus, the process of this invention will permit crudes now going to fuels to fill this gap while saving high VI solvent lube crudes for applications where their special qualities are required.
- the process of the invention involves the steps of distilling a low VI waxy crude at atmospheric pressure up to a temperature of about 650° F. to remove the distillable fraction therefrom, vacuum distilling the residue to obtain gas oil fractions and catalytically dewaxing the gas oil fractions having an SUS at 100° F. viscosity of from about 60 to about 2000 to obtain the naphthenic type lubricating oil product.
- the gas oil fractions may be hydrogenated if it is desired to improve color and/or remove nitrogen and sulfur compounds which is desirable for enhanced product quality or to avoid the adverse effects of sulfur and nitrogen on the dewaxing catalyst.
- the crude is first taken through line 11 to a still 12 and distilled at atmospheric pressure up to a temperature of about 650° F. and distillates are sent to fuels manufacture as shown by lines 13, 14 and 15.
- the residual crude is taken through line 16 to still 17 and vacuum distilled at about 25 to about 125 mm of mercury pressure (absolute) to give several gas oils of desired viscosities.
- the atmospheric and vacuum distillation columns may include caustic scrubbing zones to remove undesirable acids in the crude.
- the vacuum gas oils may next be taken through appropriate lines, shown in the FIGURE as lines 18 to 22 to an optional hydrotreater 23 and hydrotreated to improve color and remove nitrogen and sulfur compounds. Whether or not hydrotreating will be used depends on the properties of the specific crudes used along with the desired end uses for the finished lubes. If used, the operating conditions for the hydrotreating step are:
- distillates are taken through lines 24 to 28 to a dewaxer 29 where they are catalytically dewaxed to meet pour point specifications. This is accomplished by mixing the oil with hydrogen and contacting it with a catalyst at elevated temperature and pressure. Normal paraffins and nearly normal paraffins are preferentially cracked to gases and low boiling liquids which may be removed by distillation (not shown). Operating conditions are:
- the catalyst used is an alumino-silicate of the mordenite class. It must be decationized, that is Na+ ions replaced with H+ ions, to be active for this application.
- a commercially available example of H+ mordenite is Norton Company's Zeolon H.
- a group VI or VIII metal such as platinum or palladium is added to the hydrogen mordenite to give the final catalyst.
- sulfur also may be added to the H+ mordenite by using a sulfuric acid treatment before adding the group VI or VIII metal. The sulfur addition is readily accomplished by slurrying H+ mordenite with H 2 SO 4 at 90° C. for 5 hours.
- the acid laden mordenite is heated in a programmed manner to 480° C. to volatilize acid.
- Final catalyst contains at least 0.05 wt. % sulfur and more typically 2-4 wt. %.
- the catalytic dewaxing operation is preferably carried out in a fixed bed, trickle flow reactor.
- High pressure and low pressure separators remove hydrogen and hydrocarbon gases from the effluent.
- a vacuum stripper removes products of hydrocracking boiling lower than the feed. Severity is adjusted to meet the spedific pour point target of each distillate.
- Catalytic dewaxing severity would be adjusted to give the following pour points for the particular viscosity grades from the vacuum distillation:
- Nigerian Medium A specific example of the type of crude for which this invention is useful is Nigerian Medium.
- Nigerian Medium may be contrasted with naphthenic crude and high VI waxy crude as follows:
- Nigerian Medium lacks the VI potential to make a 95 VI solvent lube, but it contains wax and, thus, conventionally would only be used for fuel manufacture.
- an inexpensive lube of intermediate VI quality may be manufactured from Nigerian Medium crude.
- Other useful crudes include Trinidad Light, Garden Island Bay and Lake Washington (Louisiana Crudes), Thompson, Webster and Hawkins (Texas Crudes), which crudes contain wax and cannot by prior art methods yield 90 VI solvent lubes.
- Streams 2 through 6 were then hydrotreated using a commercially available Ni-MO catalyst (American Cyanamid HDS-9 Trilobe).
- the hydrotreating was conducted at a reactor temperature of 650° F., hydrogen pressure of 900 psig, a liquid hourly space velocity (LHSV) of 1.0, and a hydrogen recycle of 150 to 200 SCF/Bbl.
- LHSV liquid hourly space velocity
- the above hydrotreated streams were then catalytically dewaxed using a commercially available mordenite catalyst in hydrogen from (Norton Zeolon H) to which had been added 0.5% by weight of platinum.
- the dewaxing was carried out in a fixed bed trickle flow reactor operated at 550° to 600° F., a hydrogen pressure of 850 psig, liquid hourly space velocity of 0.8 to 1.0 and a hydrogen recycle of 5000 to 9000 SCF/Bbl.
- the following table shows the yields of naphthenic-type lubricating oil products obtained and their pour points.
- Streams 2 to 5 yield a product fully meeting the specifications for naphthenic type lubricating oils.
- extremely heavy grades such as stream 6 where the SUS/100° F. viscosity is 5000, the product obtained exceeds the pour point specification for the naphthenic type lubricating oils and such heavy grades from the vacuum distillation or optional hydrogenation step, rather than be subjected to catalytic dewaxing, would be used in other refinery operations or could be dewaxed by solvent dewaxing.
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- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A process for making naphthenic type lubricating oils from a low VI waxy crude which comprises distilling said low VI waxy crude to 500° to 650° F. at atmospheric pressure to separate distillable fractions therefrom, subjecting the residue to a vacuum distillation at about 25 to about 125 mm Hg absolute pressure to obtain one or more gas oil fractions, optionally hydrotreating said gas oil fractions in the presence of a Ni/Mo catalyst at 550° to 650° F., 0.25 to 1.0 LHSV, and 700-1500 psig, and catalytically dewaxing said distillates in the presence of a H+ form mordenite catalyst containing a Group VI or Group VIII metal at 550° to 750° F., 500 to 1500 psig and 0.25 to 5.0 LHSV, to obtain said naphthenic type oils having pour points of from about -60° to +20° F.
Description
Naphthenic lubricating oils are conventionally made from grade A or coastal, wax-free crudes by simple distillation of the crude in the presence of caustic. Due to such simple processing they have been relatively inexpensive.
Naphthenic oils have naturally low pour points of from -50° F. in low viscosity grades to +20° F. in high viscosity grades. Their viscosity Index (VI) is poor, but, in many applications, this quality is secondary to cost considerations. There are also some applications where the particular properties of naphthenic lubes (very low pour point and relatively high content of aromatic compounds) make them desirable in spite of any price advantage.
Solvent lubricating oils are made from waxy crudes. They require a complicated refining scheme and are, therefore, more expensive. VI is high and pour points of finished oils (after dewaxing) run 0 to +10° F. These lubes must be manufactured from selected waxy crudes, i.e., those with VI high enough to give at least 90-95 VI levels in the finished oils. Waxy crudes with lower VI potential are rejected for solvent lube manufacture and utilized only for fuels.
This invention is directed to a process for manufacturing relatively inexpensive naphthenic type lubes from the low VI waxy crudes unsuitable for solvent lubes and now used for gasoline and fuels. Such a process is desirable because reserves of grade A or coastal crudes are seriously declining and no new fields of these grades have been discovered. Thus, the process of this invention will permit crudes now going to fuels to fill this gap while saving high VI solvent lube crudes for applications where their special qualities are required.
In essence, the process of the invention involves the steps of distilling a low VI waxy crude at atmospheric pressure up to a temperature of about 650° F. to remove the distillable fraction therefrom, vacuum distilling the residue to obtain gas oil fractions and catalytically dewaxing the gas oil fractions having an SUS at 100° F. viscosity of from about 60 to about 2000 to obtain the naphthenic type lubricating oil product. Optionally, prior to the catalytic dewaxing step the gas oil fractions may be hydrogenated if it is desired to improve color and/or remove nitrogen and sulfur compounds which is desirable for enhanced product quality or to avoid the adverse effects of sulfur and nitrogen on the dewaxing catalyst.
Reference is now made to the drawing where the process of the invention is illustrated in more detail. The crude is first taken through line 11 to a still 12 and distilled at atmospheric pressure up to a temperature of about 650° F. and distillates are sent to fuels manufacture as shown by lines 13, 14 and 15. The residual crude is taken through line 16 to still 17 and vacuum distilled at about 25 to about 125 mm of mercury pressure (absolute) to give several gas oils of desired viscosities. The atmospheric and vacuum distillation columns may include caustic scrubbing zones to remove undesirable acids in the crude. The vacuum gas oils may next be taken through appropriate lines, shown in the FIGURE as lines 18 to 22 to an optional hydrotreater 23 and hydrotreated to improve color and remove nitrogen and sulfur compounds. Whether or not hydrotreating will be used depends on the properties of the specific crudes used along with the desired end uses for the finished lubes. If used, the operating conditions for the hydrotreating step are:
Temperature, °F.: 550°-650°
H2 pressure, Psig: 700-1500
LHSV: 0.25-1.0
Catalyst: Commercially available Ni-Mo
Finally, the distillates are taken through lines 24 to 28 to a dewaxer 29 where they are catalytically dewaxed to meet pour point specifications. This is accomplished by mixing the oil with hydrogen and contacting it with a catalyst at elevated temperature and pressure. Normal paraffins and nearly normal paraffins are preferentially cracked to gases and low boiling liquids which may be removed by distillation (not shown). Operating conditions are:
Temperature, °F.: 500°-750°
H2 pressure, Psig: 500-1500
LHSV: 0.25-5.0
H2 recycle, SCF/bbl: 1,000-10,000
The catalyst used is an alumino-silicate of the mordenite class. It must be decationized, that is Na+ ions replaced with H+ ions, to be active for this application. A commercially available example of H+ mordenite is Norton Company's Zeolon H. A group VI or VIII metal such as platinum or palladium is added to the hydrogen mordenite to give the final catalyst. In an alternate catalyst, sulfur also may be added to the H+ mordenite by using a sulfuric acid treatment before adding the group VI or VIII metal. The sulfur addition is readily accomplished by slurrying H+ mordenite with H2 SO4 at 90° C. for 5 hours. After filtration to remove excess H2 SO4 liquid, the acid laden mordenite is heated in a programmed manner to 480° C. to volatilize acid. Final catalyst contains at least 0.05 wt. % sulfur and more typically 2-4 wt. %.
The catalytic dewaxing operation is preferably carried out in a fixed bed, trickle flow reactor. High pressure and low pressure separators remove hydrogen and hydrocarbon gases from the effluent. A vacuum stripper removes products of hydrocracking boiling lower than the feed. Severity is adjusted to meet the spedific pour point target of each distillate.
Catalytic dewaxing severity would be adjusted to give the following pour points for the particular viscosity grades from the vacuum distillation:
______________________________________
Viscosity Grade Dewaxed Pour Point
(SUS @ 100° F.)
(F.°)
______________________________________
60 -50
100 -40
500 -10
2000 +10
______________________________________
A specific example of the type of crude for which this invention is useful is Nigerian Medium. Nigerian Medium may be contrasted with naphthenic crude and high VI waxy crude as follows:
______________________________________
Amelia A/ Zarzaitine
Perkins A
Nigerian (Typical High
(Typical
Medium VI Waxy Sol-
Naphthenic
(Low VI vent Lube
Crude) Waxy Crude)
Crude)
______________________________________
Crude Properties
°API 24.0 26.1 42
WT. % wax 0.3 3.0 4.0-5.0
650-1070° F. Fraction
Vol. % crude 36 34 22.5
WT. % wax .4-.5 8 13-15
Dewaxed satu-
rates VI 20-40 75 104
______________________________________
Nigerian Medium lacks the VI potential to make a 95 VI solvent lube, but it contains wax and, thus, conventionally would only be used for fuel manufacture. By using the process of this invention, an inexpensive lube of intermediate VI quality may be manufactured from Nigerian Medium crude. Other useful crudes include Trinidad Light, Garden Island Bay and Lake Washington (Louisiana Crudes), Thompson, Webster and Hawkins (Texas Crudes), which crudes contain wax and cannot by prior art methods yield 90 VI solvent lubes.
In order to further illustrate the invention the following examples are given:
A sample of Nigerian Medium crude was distilled in a commercial atmospheric distillation unit containing a caustic scrubbing zone to give the following streams:
______________________________________
Approx.
Stream B. Pt. (°F.)
Vol. % on Crude
______________________________________
Wet gas To 250°
6.0
Straight run gasoline
Naphtha 250°-420°
8.0
Atmospheric gas oil
420°-520°
22.0
Residue 520°+
64.0
______________________________________
The residue was then distilled in a commercial vacuum distillation unit also containing a caustic scrubber at 25 to 120 mm of mercury pressure (absolute) to give the streams shown in Table I.
TABLE I
______________________________________
Vol % D1160 VIS Ppm
Stream
of Distill, °F.
SUS/ Sul- Pour D-1500
No. Crude 10% 90% °API
100° F.
fur Pt. Color
______________________________________
1 13.0 -- -- -- -- -- -- --
2 3.5 578 707 23.9 64 2000 +12 1.0
3 11.0 608 787 22.8 124 1700 +44 1.75
4 5.0 704 871 20.7 560 2400 +71 2.75
5 11.0 773 956 18.9 2000 2400 +88 4.0
6 5.0 813 1064 18.1 5000 3200 +94 6.5
Caustic
2.0 -- -- -- -- -- -- --
Sludge
Vac- 13.5 -- -- -- -- -- -- --
Resi-
due
______________________________________
Streams 2 through 6 were then hydrotreated using a commercially available Ni-MO catalyst (American Cyanamid HDS-9 Trilobe). The hydrotreating was conducted at a reactor temperature of 650° F., hydrogen pressure of 900 psig, a liquid hourly space velocity (LHSV) of 1.0, and a hydrogen recycle of 150 to 200 SCF/Bbl. After hydrotreating the sulfur content was seen to have been reduced and color was improved while pour point remained the same. The properties of the streams from the hydrotreater are shown in the following table:
______________________________________
Ppm D 1500 Pour
Stream Sulfur Color Point of
______________________________________
2 96 0.75 +12
3 225 1.25 +42
4 393 1.50 +70
5 503 2.25 +88
6 626 2.75 +94
______________________________________
The above hydrotreated streams were then catalytically dewaxed using a commercially available mordenite catalyst in hydrogen from (Norton Zeolon H) to which had been added 0.5% by weight of platinum. The dewaxing was carried out in a fixed bed trickle flow reactor operated at 550° to 600° F., a hydrogen pressure of 850 psig, liquid hourly space velocity of 0.8 to 1.0 and a hydrogen recycle of 5000 to 9000 SCF/Bbl. The following table shows the yields of naphthenic-type lubricating oil products obtained and their pour points.
______________________________________
Yield, Wt. % of Charge Product
Stream C.sub.1 -C.sub.5
C.sub.5 -IBP
IBP Pour Pt. °F.
______________________________________
2 3.5 4.5 92.0 -60
3 2.0 2.0 96.0 -40
4 5.0 3.0 92.0 -30
5 2.5 3.0 94.5 +08
6 1.5 0.5 98.0 70
______________________________________
As can be seen from the above table, Streams 2 to 5 yield a product fully meeting the specifications for naphthenic type lubricating oils. With extremely heavy grades such as stream 6 where the SUS/100° F. viscosity is 5000, the product obtained exceeds the pour point specification for the naphthenic type lubricating oils and such heavy grades from the vacuum distillation or optional hydrogenation step, rather than be subjected to catalytic dewaxing, would be used in other refinery operations or could be dewaxed by solvent dewaxing.
Claims (6)
1. A process for making naphthenic type lubricating oils from a low VI waxy crude .Iadd.unsuitable for solvent lubes .Iaddend.which consists of distilling said low VI waxy crude to 500° to 650° F. at atmospheric pressure to separate distillable fractions therefrom, subjecting .Iadd.all of .Iaddend.the residue to a vacuum distillation at about 25 to about 125 mm Hg absolute pressure to obtain one or more distillate fractions having an SUS at 100° F. viscosity of from about 60 to about 2000, and catalytically dewaxing .[.all of.]. said .[.distillates.]. .Iadd.distillate fractions .Iaddend.in the presence of an H+ form mordenite catalyst containing a Group VI or Group VIII metal at 550° to 750° F., 500 to 1500 psig and 0.25 to 5.0 LHSV to obtain said naphthenic type oils having a pour point of from about -50° to +20° F.
2. The process of claim 1 where the low VI waxy crude is Nigerian Medium.
3. The process of claim 1 where catalytic dewaxing is carried out in a fixed bed, trickle flow reactor.
4. The process of claim 1 where sulfur is added to the H+ mordenite catalyst.
5. A process for making naphthenic type lubricating oils .[.fom.]. .Iadd.from .Iaddend.a VI waxy crude which consists of atmospherically distilling said crude to remove wet gas, straight run gasoline, naphtha and atmospheric gas oil fractions, subjecting the residue to a vacuum distillation at about 25 to 120 mm mercury pressure absolute to obtain gas oil fractions having an SUS at 100° F. viscosity of from about 60 to about 2000, hydrotreating said gas oil fractions in the presence of a Ni/Mo catalyst at about 650° F., a hydrogen pressure of about 800 psig and a LHSV of about 1.0, and catalytically dewaxing said hydrotreated gas oil fractions in the presence of an H+ form mordenite catalyst containing platinum at a temperature of about 550° to about 600° F., a hydrogen pressure of about 850 psig, and a LHSV of from about 0.8 to about 1.0 to obtain naphthenic type oils having a pour point of from about -60° to about 20° F.
6. The process of claim 5 where the low VI waxy crude is Nigerian Medium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/078,616 USRE30529E (en) | 1979-09-24 | 1979-09-24 | Manufacture of naphthenic type lubricating oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/078,616 USRE30529E (en) | 1979-09-24 | 1979-09-24 | Manufacture of naphthenic type lubricating oils |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US05/754,284 Reissue US4100056A (en) | 1976-12-27 | 1976-12-27 | Manufacture of naphthenic type lubricating oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| USRE30529E true USRE30529E (en) | 1981-02-24 |
Family
ID=22145193
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US06/078,616 Expired - Lifetime USRE30529E (en) | 1979-09-24 | 1979-09-24 | Manufacture of naphthenic type lubricating oils |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | USRE30529E (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4515680A (en) * | 1983-05-16 | 1985-05-07 | Ashland Oil, Inc. | Naphthenic lube oils |
| US10087379B2 (en) | 2014-09-17 | 2018-10-02 | Ergon, Inc. | Process for producing naphthenic base oils |
| US10479949B2 (en) | 2014-09-17 | 2019-11-19 | Ergon, Inc. | Process for producing naphthenic bright stocks |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3902988A (en) * | 1973-02-09 | 1975-09-02 | British Petroleum Co | Production of lubricating oils |
| US3926786A (en) * | 1972-11-20 | 1975-12-16 | Texaco Inc | Production of lubricating oils |
| US3929616A (en) * | 1974-06-26 | 1975-12-30 | Texaco Inc | Manufacture of lubricating oils |
-
1979
- 1979-09-24 US US06/078,616 patent/USRE30529E/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3926786A (en) * | 1972-11-20 | 1975-12-16 | Texaco Inc | Production of lubricating oils |
| US3902988A (en) * | 1973-02-09 | 1975-09-02 | British Petroleum Co | Production of lubricating oils |
| US3929616A (en) * | 1974-06-26 | 1975-12-30 | Texaco Inc | Manufacture of lubricating oils |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4515680A (en) * | 1983-05-16 | 1985-05-07 | Ashland Oil, Inc. | Naphthenic lube oils |
| US10087379B2 (en) | 2014-09-17 | 2018-10-02 | Ergon, Inc. | Process for producing naphthenic base oils |
| US10479949B2 (en) | 2014-09-17 | 2019-11-19 | Ergon, Inc. | Process for producing naphthenic bright stocks |
| US10557093B2 (en) | 2014-09-17 | 2020-02-11 | Ergon, Inc. | Process for producing naphthenic base oils |
| US10800985B2 (en) | 2014-09-17 | 2020-10-13 | Ergon, Inc. | Process for producing naphthenic bright stocks |
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