CA1228563A - Use of high pressure to improve product quality and increase cycle length in catalytic lube dewaxing - Google Patents

Abstract

USE Of HIGH PRESSURE TO IMPROVE PRODUCT QUALITY AND
INCREASE CYCLE LENGTH IN CATALYTIC LUBE DEWAXING

ABSTRACT

A process for preparing high quality lube base stock oil from waxy crude oil is provided which comprises separating from the waxy crude a distillate fraction thereof having an initial boiling point of at least 232°C (450°F) and a final boiling point labs than 566°C (1050°F), extracting the distillate fraction with a solvent selective for aromatic hydrocarbons to yield a raffinate from which undesirable compounds have been removed, catalytically dewaxing the raffinate in the presence of hydrogen to a pour point not higher than -1°C (+30°F) by contacting the raffinate at a temperature of 260°C to 385°C (500° to 725°F) at a hydrogen partial pressure of above 10350 kPa (1500 psia) in the absence of hydrotreating catalyst with a dewaxing catalyst comprising an aluminosilicate zeolite having a silica/alumina ratio above 12 and a constraint index of from 1 to 12 thereby forming dewaxed raffinate and lower boiling hydrocarbons, and topping the raffinate subsequent to dewaxing to remove therefrom the lower boiling hydrocarbons, thereby directly recovering substantially all of the remainder of the dewaxed raffinate, the remainder having a pour point not higher than -1°C (+30°F).

Description

~L~2~S6~3 USE OF HIGH PRESSURE TO IMPROVE PRODUCT QUALITY AND
INCREASE CYCLE LENGTH IN CATALYTIC LUBE DEW AXING

This invention relates to the manufacture of high grade viscous oil products from crude petroleum fractions, particularly high quality lube base stock oils from crude stocks of high wax content, commonly classified as "wax base" as compared with the "naphthenic base" crudest The latter cruxes are relatively lean in straight chain paraffins and yield viscous fractions which inherently possess low pour points.
lo A process for preparing high quality lube base stock oil from waxy crude oil which comprises separating from the waxy crude a distillate fraction thereof having an initial boiling point of at least 232C (450F) and a final boiling point less than 566qC
(105ûF~, extracting the distillate fraction with a solvent selective or aromatic hydrocarbons to yield a raffinate from which undesirable compounds have been removed, catalytically dew axing the rafFinate in the presence of hydrogen to a pour point not higher than -1C (+30F) by contacting theraf~înate at a temperature of 260 to 385C (50û to 725F) at a hydrogen partial pressure of I 10,350 spa (1,500 Asia) in the absence of hydrotreating catalyst with a dew axing catalyst comprising an al~ninosllicate zealot having a silica/alumina ratio above 12 and a constraint index between 1 and 12 thereby worming dockside raffinate and lower boiling hydrocarbons, and topping the raffinate subsequent to dew axing to I remove therefrom the lower boiling hydrocarbons, directly recovering substantially all of the remainder of the dockside raffinate, the remainder having a pour point not higher than -1C (~30~f).
High quality lube base stock oils are conventionally prepared by refining distillate fractions or the residuum prepared I by vacuum distilling a suitable crude oil from which the lighter portion has been removed Dye distillation in an atmospheric tower.
Titus, the charge up the vacuum tower is commonly referred to as a "long residuum," and the residuum from the vacuum tower is ~228S~
f-1886 -2-distinguished from the starting material by referring to it as the "short residuum."
The vacuum distillate fractions are upgraded by a sequence of unit operations, the first of which is solvent extraction with a solvent selective for aromatic hydrocarbons. This step serves to remove aromatic hydrocarbons of low viscosity index and provides a raFfinate of improved viscosity index and quality. Various processes have been used in this extraction stage, and these employ solvents such as furfural, phenol, sulfur dioxide and others. The I short residuum, because it contains most of the asphaltenes of the crude oil, is conventionally treated to remove these asphalt-like constituents prior to solvent extraction to increase the viscosity index.
The raffinate from the solvent extraction step contains paraffins which adversely affect the pour point. Thus, the waxy raffinate~ regardless of whether prepared from a distillate fraction or from the short residuum, must be dockside. Various dew axing procedures have been used and the art has gone in the direction of treatment with a solvent such as methyl ethyl kitten (~K)Jtoluene mixtures to remove the wax and prepare a dockside raffinate. The dockside raffinate may then be finished by any of a number of sorption or catalytic processes to improve color and oxidation stability.
The quality of the lube base stock oil prepared my the sequence of operations outlined above depends on the particular crude chosen as well as the severity of treatment for each of the treatment steps. additionally, the yield of high quality lube base stock oil also depends on these factors and, as a rule, the higher the quality sought, the less the yield. In general, naphthenic cruxes are savored because less loss is encountered, particularly in the dew axing step. In many cases, however, waxy cruxes are more readily available and it would be desirable to provide a process for preparing high quality lube base stock oils in good yields from such waxy crude oils.

In recent years, processes for the selective hydrocracking of paraffinic components to lower molecular weight fragments employing a zealot catalyst have been developed to accomplish the dew axing of crude stocks of high wax content. thus, for example, the lube oil dew axing process of US. Patent No. 3,337,447 utilizes a cadmium containing Zealot A catalyst. In accordance with US.
Patent No. 3,438,887, improved lubricating oils are prepared from waxy distillates by a sequence of solvent refining, catalytic dew axing over tune low sodium or acid form of mordant containing a Ill hydrogenating component such as a Group VIII metal and hydrofining.Similar catalytic dew axing processes are described in US. Patent ooze. 3,539,498 and 3,684,684. The lube oil dew axing process of US.
Patent No. 3~620,963 employs a catalytic mixture of mordant and a nickel-tin component.
lo Lately, the dew axing of solvent refined waxy crude to provide high quality lube base stocks employing an aluminosilicate zealot having a silica to alumina ratio greater than 12 and a constraint index of 1 to 12 as represented by the ZSM-5 class of zealots has cove into prominence. Illustrative of the foregoing is MU the combined catalytic dewaxing~catalytic hydrotreating process described in US. Patent No. 4,137,148~ In accordance with this process, a fraction having an initial boiling point of at least awoke (450f) and a final boiling point less than 566C (1050F) is taken by distillation of a Sax base crude. That fraction is solvent refined by counter current extraction with at least an equal volume of a selective solvent such as furfural. The fur~ural raffinate is subjected to catalytic dew axing by mixing with hydrogen and contacting at 260-357C (500-615F) with a catalyst containing a hydrogenation metal and zealot ZSM-5 or other aluminosilicate zealot having a silica/alumina ratio above 12 and a constraint index of 1 to 12 and space velocity (LHSV) of 0.1 to I volumes of charge oil per volume of catalyst per hour. The effluent a catalytic dew axing is then cascaded into a hydrotreater containing, as catalyst, a hydrogenation component on a non-acidic support, such as cobalt-molybdate or nickel-molybdate on alumina. The hydro-treater operates at 218 to 316C (425 to 600F), preferably 246 to 288C (475 to 550F), and space velocity like that of the catalytic dew axing reactor. The reactions are carried out at hydrogen partial pressures of 1035-10350 spa (150-1500 Asia), at the reactor inlets, and preferably at 1725-3450 spa ~250-500 Asia), with 89 to 890 1/1 (500 to 5000 standard cubic feet) of hydrogen per barrel of feed SCAB preferably 267 to 445 1/1 ~1500 to 2500 Scab I The hydrotreating step of the process of US. Patent No.
4,137,148 is essential if a lube base stock oil possessing adequate oxidation stability is to be obtained. In addition to the requirement of a hydrotreating step, it is necsssarv to reactivate the catalyst in this process before lined-out temperature operation is achieved since the lined out temperature at the aforestated operating pressures is well above 357JC (fly i.e., a temperature at which the oxidation stability of the final product begins to fall o M significantly.
It has now been discovered that by operating within a MU hydrogen partial pressure regime of at least 10~50 spa (1500 Asia), dew axing of a solvent refined wax base crude to provide a high quality lube base stock oil can be accomplished whatnot the need for a separate hydrotreating step or hydrotreating catalyst as in US.
Patent No. 47137l148, eye-I In addition to sliminatirg the requirement for a separate hydrotreating step, the present process results in a significant lowering of the line-out temperature thereby extending catalyst life and reducing the frequency with which the dealing catalyst must be regenerated.
I The wax base cruxes (sometimes called paraffin oases") from which the charge stock< is derived by distillation constitute a wall recognized class of crude petroleums. zany scales have been devised for classification of crude, some of which are described in Chapter YIP Evaluation of Oil Stocks a "Petroleum Refinery Engineering," WYLIE. Nelson, McGraw-Hill, 1941. A convenient scale identified by Nelson at page 69 involves determination of the cloud point of the Bureau of Mines "Key Fraction No. 2" which boils between 275C and 300C (527F and 57~F) at 40 mm pressure. If the cloud point of this fraction is above -15C (5F), the crude is considered to be wax base.
According to the present invention, a propane disaffiliated short residuum fraction or a fraction having an initial boiling point of at least 232C (450F) and a final boiling point less than lo 566C (1050F) is prepared by distillation of such wax base crude.
That fraction is solvent refined by counter current extraction with at least an equal volume (100 vowel) of a selective solvent such as fu~fural. It is preferred to use from 1.5 to 3.0 volumes of solvent per volume of oil. The fur~ural raffinate is subjected to catalytic dew axing by mixing with hydrogen and contacting at 260-385C
(500-725F) and a hydrogen partial pressure of above 10~50 spa (1,500 Asia) and preferably at least 1~800 spa (2,000 Asia) with a catalyst containing a hydrogenation metal and zealot ZS~-5 or other aluminosilicate zealot having a silicaJalumina ratio above 12 and a constraint index of 1 to 12 and preferably a hydrogenation component, using a liquid hourly space velocity (LHSV) of I to 2.0 volumes of charge oil per volume of catalyst per hour. The preferred space velocity is 0.5 to lo L~SV.
In some instances it may be desirable to partially Dixie the charge stock, i.e., solvent-extracted raffinate, by conventional solvent dew axing techniques, for example, to a pour point of from -12C (10F) to 10C (50F). The higher melting point waxes so removed are those ox higher market value than the waxes removed in I conventionally taking the product to a still lower pour point below -12C (10F).
The cracked (and hydrogenated) fragments from cracking wax molecules in the catalytic dewaxer will have adverse effects on flash and fire points of the dockside raffinate product and are it therefore removed by distillation ox the product to meet flash and fire point specifications.

The catalyst employed in the catalytic dew axing reactor and the temperature in that reactor are important to success in obtaining good yields and very low pour point product. The hydrotreater catalyst may be any of the catalysts commercially S available for that purpose but the temperature should be held within narrow limits for best results.
The solvent extraction technique is well understood in the art and needs no detailed review here. The severity of extraction is adjusted to the composition of the charge stock to meet I specifications for the particular lube base stock and the contemplated end-use. This severity will be determined in practice of this invention in accordance with well established practices.
The dew axing catalyst is a composite of hydrogenation metal, preferably a metal of Group VIII of the Periodic Table, associated with the acid form of a novel class of aluminosilicate zealot having a silicafalumina ratio ox at least about 12 and a constrained access to the intrac~ystalllne free space, as more fully described hereinbelow.
An important characteristic of the crystal structure of I this class of zealots is that it provides constrained access to and egress prom thy intracrystalline free space by virtue of having a pore dimension greater than 5 Angstroms and pore windows of about a size such as lulled be provided by 10-membered rings of oxygen atoms. It is to be understood, of course/ that these rings are I those formed by the regular disposition of the tetrahedral making up the anionic framework of the crystalline aluminosilicate, the oxygen atoms themselves being bonded to the silicon or aluminum atoms at the centers of the tetrahedral briefly, the preferred type zealots useful in this invention possess, in combination: a silica to I) alumina mole ratio of at least 12; and a structure providing constrained access to the crystalline free space.
The silica to alumina ratio referred to may be determined by conventional analysis. This ratio is meant to represent, as closely as possible, the ratio in the rigid anionic framework of toe LO it zealot crystal and to exclude aluminum in the binder or in cat ionic or other form within the channels. Although zealots with a silica to alumina ratio of at least 12 are useful, it is preferred to use zealots having higher ratios of at least 30. Such zealots, after activation acquire an intracrystalline sorption capacity for normal hexane which is greater than that for water, i.e., they exhibit "hydrophobic" properties. It is believed that this hydrophobic character is advantageous in the present invention.
The type zealots useful in this invention freely sorb I normal hexane and have a pore dimension greater than about 5 Angstroms. In addition, the structure must provide constrained access to larger molecules. It is sometimes possible to judge from a known crystal structure whether such constrained access exists.
For example, if the only pore windows in a crystal are formed by 8-membered rings of oxygen atoms, then access by molecules of larger cross-section than normal hexane is excluded and the zealot is not of the desired type. 'windows of lO-membered rings are preferred, although, in some instances, excessive puckering or pore blockage may render these zealots ineffective Twelve-membered rings do not generally appear to offer sufficient constraint to produce the advantageous conversions, although puckered structures exist such as TEA offretite which is a known effective zealot. Also, structures can be conceived, due to pore blockage or other cause, that may be operative.
Rather than attempt to judge from crystal structure whether or not a zealot possesses the necessary constrained access, a simple determination of the "constraint index" may be made by passing continuously a mixture of an equal weight of normal hexane and 3-methylpentane over a small sample, approximately 1 gram or I less, of catalyst at atmospheric pressure according to the followingprocedure. A sample of the zealot, in the for of pellets or extradite, is crushed to a particle size about that of coarse sand and mounted in a glass tube. Prior to testing, the zealot it treated with a stream of air at 538C (1000F) for at least 15 I
F-1886 ~~~

minutes. The zealot is then flushes with helium and the temperature adjusted between 288C and 510C (550F and 950F) to give an overall conversion between lay and 60%. The mixture of hydrocarbons is passed at 1 liquid hourly space velocity (i.e., 1 volume of liquid hydrocarbon per volume of zealot per hour) over the zealot with a helium dilution to give a helium to total hydrocarbon mole ratio of 4:1. After 20 minutes on stream, a sample of the effluent is taken and analyzed, most conveniently by gas chromatography, to determine the fraction remaining unchanged for I each of the two hydrocarbons.
The "constraint index" is calculated as follows:

1910 (f_ cation of Nixon rem_ininq) Constraint Index =
loglo(fraction of 3-methylpentane remaining) The constraint index approximates the ratio of the cracking rate constants or the two hydrocarbons. Zealots suitable for the present invention are those having a constraint index in the approximate range of 1 to 12. Constraint Index (I) values for some typical zealots are.

CAY KIWI.
ZSM-5 8.3 I ZSM-ll 8.7 ZSM~lZ 2 ZSM~5 4 5 TEA Offretite 3.7 Beta 0.6 H-Zeolon 0.4 Amorphous Silica-Alumina 0.6 Errant 38 _____ ~22~ 3 It is to be realized that the above constraint index values typically characterize the specified zealots but that such are the cumulative result of several variables used in determination and calculation thereof. Thus, for a given zealot depending on the temperature employed within the affronted range of 260 to 51ûC
(500~ to 950f), with accompanying conversion between lug% and owe, the constraint index may vary within the indicated approximate range of 1 to 12. Likewise, other variables such as the crystal size of the zealot, the presence of possible occluded contaminants and Ill binders intimately combined with the zealot may affect the constraint index. It will accordingly be understood by those skilled in the art that the constraint index, as utilized herein, while affording a highly useful means for characterizing the zealots of interest is approximate, taking into consideration the manner ox its determination, with probability, in some instances, of compounding variable extremes. Ho~vever1 in all instances at a temperature within the above-specified raitge of ~88Q to ~10C (55CF
to 95ûf), the constraint index will have a value for any given zealot of interest herein within the approximate range ox 1 to 12.
The class of zealots defined herein is exemplified my ZSM-5, ZSM-ll, ZSM-12, ZSM-35, ZSM 38, and other similar materials.
US. Patent No. 3,702,886 describes ZSM-5, ZSM-ll is described in US. Patent No. 3,709,979,ZSM-12 is described in US. Patent No.
7,832,449, ZSM-35 is described in US. Patent No. 4,0169245, and ZSM-38 is described in US. Patent No. 4,046,859.
The specific zealots described, when prepared in the presence of organic cations, are catalytically inactive, possibly because the intracrystalline free space is occupied by organic cations from the forming solution. they may be activated by heating MU in an inert atmosphere at 538C (1000F) for one hour, for expel, followed by base exchange with ammonium salts followed by calcination at 38C (100F) in air. The presence of organic cations in the forming solution may not be absolutely essential to the formation of this type zealot; however, the presence of these I
F~1886 -10-cations does appear to favor the formation of this special type of zealot. More generally, it is desirable to activate this type catalyst by base exchange with ammonium salts followed by calcination in air at about 538C (1000F) for from 15 minutes to 24 hours.
Natural zealots may sometimes be converted to this type zealot catalyst by various activation procedures and other treatments such as base exchange, steaming, alumina extraction and lo calcination, in combinations. Natural minerals which may be so treated include ferrerite, brewsterite, stilbite, dachiardite, epistilbite, heulandite, and clinoptilolite. The preferred crystalline aluminosilicates are ZSM-5, ZSM-ll, ZSM-12, ZSM-38 and ZSM-35, with ZSM-5 particularly preferred.
In a preferred aspect of this invention, the zealots hereof are selected as those having a crystal framework density, in the dry hydrogen Form, of not substantially below 1.6 grams per cubic centimeter. It has been found that zealots which satisfy all three of these criteria are most desired. Therefore, the preferred Z0 zealots of this invention are those having a constraint index as defined above of from 1 to 12, a silica to alumina ratio of at least about 12 and a dried crystal density ox not less than about 1.6 grams per cubic centimeter. The dry density for known structures may be calculated from the number of silicon plus aluminum atoms per Lowe cubic Angstroms, as given, ego on page 19 of the article on Zealot Structure by WOMB. Meter from "Proceedings of the Conference on Molecular Sieves, London, April 1967," published by the Society of Chemical Industry, London? 1968. When the crystal structure is unknown, the crystal framework density may be determined by I classical pycnometer techniques. For example, it may be determined by immersing the dry hydrogen Norm of the zealot yin an organic solvent which is not sorted by the crystal. It is possible that thy unusual sustained activity and stability of this class of zealots is associated with its high crystal anionic Framework density of not less than about 1.6 grams per cubic centimeter. This high density, I
F-1886 -11~

of course, must be associated with a relatively small amount of free space within the crystal, which might be expected to result in more stable structures. This free space, however, is important as the locus of catalytic activity.
Crystal framework densities of some typical zealots are:

Void Framework Zealot Volume _ Density Ferrierite0.28 cc/cc 1.76 g/cc Mordant .28 1.7 I ZSM-5, -11 .29 1.79 ~achiardite .32 1.72 L .32 1.61 Clinoptilolite.34 1.71 Laminate .34 1.77 ZSM-4 (Omega) .38 1.65 Heulandite .39 1.69 P .41 1.57 Offretite .41 1.55 Levynite .41 1.54 I Errant .35 1.51 Gmelinite .44 1.46 Shabbiest .47 1.45 A .5 1.3 Y .48 1.27 When synthesized in the alkali metal form, the zealot is conveniently converted to the hydrogen form generally by intermediate formation of the ammonium form as a result of Amman ion exchange and calcination of the ammonium form to yield the hydrogen form. In addition to the hydrogen form, other forms of the Jo zealot wherein the original alkali metal has been reduced to less than about 1.5 percent by weight may be used. Thus, the original alkali metal of the zealot may be replaced by ion exchange with other suitable ions of Groups IT to VIII of the Periodic Table, including, for example, nickel, copper, zinc, palladium, calcium or rare earth metals.
In practicing the desired conversion process, it may be desirable to incorporate the above described crystalline aluminosilicate zealot in another material resistant to the temperature and other conditions employed in the process. Such Ill matrix materials include synthetic or naturally occurrir~ substances as well as inorganic materials such as clay, silica and/or metal oxides. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Naturally occurring clays which can be composite with the zealot include those of the montmorillonite and kaolin Allis, which families include the sub-bentonites and the kaolin commonly known as Dixie, McNamee-Georgia and Florida clays or others in which the main mineral constituent is hollowest, coolant, Dakota, nacrite or anxiety. Such clays can be used in the raw I state as originally mined or initially sub~eoted to calcination, acid treatment or chemical modification.
In addition to the foregoing materials, the zealots employed herein may be composite with a porous matrix material such as alumina, silica-alumina, silica-magnesia, siiica~zirconia, I silica-thoria, silica-berylia, silica-titania as well as ternary compositions, such as silica-alumina-thoria, silica-alumina-zirconia, silica-alurnina-magnesia and silica-magnesia-zirconia. The matrix may be in the form of a Vogel. The relative proportions of zealot component and inorganic I oxide gel matrix may vary idyll with the zealots corltallt ranging from 1 to 99 percent by weight and more usually in the range ox` prom 5 to 80 percent by weight of the composite.

~2~63 The effluent of the dew axing unit is topped by distillation, i.e., the most volatile components are removed, to meet flash and fire point specifications While a hydrotreating step such as that described in US.
Patent No. 4,137,148, swooper, is ordinarily not required to provide a lube base stock oil having a suitable level of oxidation stability, in some cases it may be desirable to conduct such a step herein. In such case, the catalytic dew axing effluent is introduced into a hydrotreater containing, as catalyst, a hydrogenation component on a It) non-acidic support, such as cobalt-molybdate or nickel-molybdate on alumina. Hydrotreating is effected therein at a temperature of from about 218 to 316C (425 to Coffey), hydrogen partial pressures of 10~5-10350 spa (150-1500 Asia), at the reactor inlets, and preferably 1725-3450 spa (250-500 Asia), with By to 890 lo (500 to 5000 standard cubic feet) ox hydrogen per barrel of feed SCAB
preferably 267 to 445 1~1 (1500 to 2500 S~F/3).
The following examples illustrate the present invention.
In the examples, all parts given are by weight unless specified otherwise.

Examples l to 4 illustrate of the high-p~essure catalytic dew axing process of the present invention carried out upon two heavy neutral lube stocks, designated Ra~finate A and Raffinate B, and Example 5 illustrates a low-pressure combined catalytic Z5 dewaxing/hydrotreating process such as described in US. Patent No.
4,1~7,148. In all examples, a nickel-containing Whom catalyst was employed.

~228~

Raffinates A and B possessed the properties set worth in Table I as follows:

TALE

Fist Raf~inate A
Gravity, APE 29.7 29.4 Pour Point C (OF) 46 (115) 49 (120) Hydrogen, wit % 13.70 13.63 Sulfur, wit % 0.85 0 76 lo Nitrogen, wit % 0.03 0.03 Basic Nitrogen, Pam 47 30 CUR, wit% 0.06 OOZE
TV, at 100C, US 9.4 11.1 Distillation IMP 423 (793) was t766) 5% ~54 (aye ~71 t879~
lo 46~ (864) 4~3 (~02) owe 480 I 501 (g34) 50% 494 (g21~ 510 go I I 508 (g47) 521 ~969j pa% ~19 (966) aye (980 95~ 545 tlO13) 544 (1012) The process conditions and yields for each example are set forth in Table II as follows:

~2~5~i~

TABLE If Process Conditions and Yields -(to -7C (20F _ r Point EXAMPLE

Operating Conditions 1 2 3 4 5 Raffinate A A A B A
Pressure, spa 13,80013,800 13,800 13,800 2,760 Asia 2,0002,000 2,000 2,000 400 Temperature, C 304 362 369 371 303 LHSV 0.98 0.98 0.98 0.93 1.0 Catalyst Age, days on stream 4.7 17 23 30 --Ho Circulation, 1~1 395.2477.0 aye 42504 398.7 scab 2,2202,680 2,710 guy 2,240 Process Yields H25, Wit% 0.14 0.28 0.36 0.31 0.22 NH3, White 0 0 0 0 0 Cluck' Wit% I r 15 5.28 5.75 2.7 C4, Wit% 6.22 5~52 I 6.~6~ 5.8 C5, Wit% ~.16 4.36 4.24 3.06 4.5 C6-166C(330F) 4.80 3.05 2.49 2.54 5.7 166~C-343C
~330-650~f) 3.32 4.79 4.65 5.07 343C~(650~F~ 77.8979.37 75.02 76.96 81.5 royal loo Lowe. 52 100.72 100.34 100.1 Hydrogen Consumption, I scab 185 300 415 197 115

Claims (8)

CLAIMS:

1. A process for preparing high quality lube base stock oil from waxy crude oil which comprises separating from the waxy crude a distillate fraction thereof having an initial boiling point of at least 232°C (450°F) and a final boiling point less than 566°C
(1050°F), extracting the distillate fraction with a solvent selective for aromatic hydrocarbons to yield a raffinate from which undesirable compounds have been removed, catalytically dewaxing the raffinate in the presence of hydrogen to a pour point not higher than -1°C (+30°F) by contacting theraffinate at a temperature of 260° to 385°C (500° to 725°F) at a hydrogen partial pressure of 10,350 kPa (1,500 psia) in the absence of hydrotreating catalyst with a dewaxing catalyst comprising an aluminosilicate zeolite having a silica/alumina ratio above 12 and a constraint index between 1 and 12 thereby forming dewaxed raffinate and lower boiling hydrocarbons, and topping the raffinate subsequent to dewaxing to remove therefrom the lower boiling hydrocarbons, directly recovering substantially all of the remainder of the dewaxed raffinate, the remainder having a pour point not higher than -1°C (+30°F).

2. The process of to Claim 1 wherein the dewaxing catalyst comprises an aluminosilicate zeolite and a hydrogenation metal.

3. The process of Claim 2 wherein the aluminosilicate zeolite is ZSM-5.

4. The process of Claim 1, 2 or 3 wherein a hydrogen partial pressure of at least 13800 kPa (2,000 psia) is employed.

5. The process of Claim 1, 2 or 3 wherein the effluent of the catalytic dewaxing step is subjected to hydrotreating.

6. The process of Claim 1, 2 or 3 wherein the raffinate is partially dewaxed by solvent dewaxing before the catalytic dewaxing step.

7. The process of Claim 1, 2 or 3 wherein the raffinate is catalytically dewaxed to a pour point not higher than about 4°C (40°F), and wherein the remainder of the directly recovered dewaxed raffinate has a pour point of not higher than 4°C
(40°F).

8. A process according to Claim 1 wherein the effluent of the dewaxing step is subjected to hydrotreating.