SEPARATION OF DEWAXING SOLVENT FROM DEWAXED OIL IN A LUBE OIL DEWAXING PROCESS USING ASYMMETRIC POLYIMIDE MEMBRANES

Abstract: Dewaxing solvents, particularly ketone solvents and ketone/toluene solvents, are separated from a mixture of dewaxing solvents and dewaxed oil in a lube oil dewaxing process by use of an asymmetric permselective polyimide membrane. Said asymmetric polyimide membrane permits the selective permeation of the ketone or ketone/toluene dewaxing solvents while being less permeable to oil. Said separation is conducted by contacting the ketone or ketone/­ toluene solvent/oil mixture with the dense side [(1),] of the asymmetric polyimide membrane [(4),] under pressure. The recovered ketone or ketone/toluene solvent is of high enough purity to be returned to the dewaxing process without further treatment. The recovered oil is passed to sub­ sequent conventional treatment means (e.g., distillation) for removal of any ketone or ketone/toluene solvent remaining therein.

Description: DESCRIPTION OF THE INVENTION The solvent dewaxing of waxy hydrocarbon oils wherein the waxy oil is contacted with a dewaxing solvent, cooled to precipitate the wax, the solvent/oil wax slurry is separated into a wax stream and a solvent/oil stream and the solvent/oil stream is separated into a solvent stream and an oil stream, is improved by performing part of the separation of the dewaxing solvent/oil stream using a selective permeat ion barrier consisting of an asymmetric polyimide membrane, preferably prepared from the class of aromatic, fully imidized polyimide polymers, followed by distillation to recover the remainder of the solvent. The dewaxing solvent/oil mixture is contacted with the dense side of an asymmetric polyimide membrane under reverse osmosis conditions, i.e., under a pressure at least sufficient to overcome the osmotic pressure of the solution. The dewaxing solvent selectively permeates through the membrane while the bulk of the oil is rejected by the membrane. In this manner an effective and energy efficient partial separation of the dewaxing solvent from the oil is made. This dewaxing solvent recovered by permeation through the membrane, is of sufficiently high purity to be returned to the dewaxing process with no additional treatment. The retentate from the membrane is passed to conventional upgrading means, such as distillation, wherein the dewaxing solvent remaining with the oil following the membrane separation is removed. Since a substantial volume of dewaxing solvent will have been removed from the solvent/oil stream by use of the asymmetric polyimide membrane the retentate stream has a much reduced concentration of dewaxing solvent (residual solvent) and less energy will be c"ns'jmed in the form e.g., of distillation or solvent stripping to remove that residual solvent to yield pure oil. Utilization of the polyimide membrane separation process of the present invention will allow a significant increase in the thru-put of the dewaxer system. Asymmetric polyimide membranes are capable of functioning as low cost modules inserted into the processing flow stream either supplementing the conventional hardware already in place in old constructions (thereby increasing thruput or debottlenecking a given unit), or in new plants supplementing conventional hardware (thereby reducing the amount of conventional hardware installed). The asymmetric polyimide membranes used in the process of the present invention are polyimide membranes characterized as being semipermeable and of the reverse osmosis type. USP 4,307,135 assigned to MSI describes one such membrane having the ability to remove NaCi from a NaCl-water solution, such NaCl rejection being in the 95 to 99+t range. DESCRIPTION OF THE FIGURES Figure 1 describes a fabric supported asymmetric polyimide membrane. Figure 2 describes a specific debasing operation employing solvent recovery using asymmetric polyimide membrane. The structure of the asymmetric reverse osmosis polyimide membrane is shown in Figure 1 for a specific embodiment. It consists of a support fabric (3) onto which is formed the membrane (4). The support fabric represented as a woven cloth support may be, in practice, any readily permeable material (one which does not hinder or interfere with the flow of the permeate) and which is compatible with the solvent and the oil system, i.e., does not dissolve under the conditions of use. Therefore, in addition to the woven cloth support represented, one may also use similar materials which merely serve as a backing and support for the asymmetric reverse osmosis polyimide membrane, e.g., metal mesh, sintered metal, porous ceramic, sintered glass, paper, porous nondissolving plastic, etc. In practice it is preferred that the support backing material be a woven or non woven cloth, representative fiber materials being nylon, polyester, polypropylene, polyethylene or high wet strength paper. The reverse osmosis polyimide membrane is described as being asymmetric, that is, the membrane is not uniform throughout its crosssection. It consists of a thin, dense layer (active layer) (1) formed atop a porous layer (2). This asymmetric membrane is supported on a backing material. The thinner the active layer the lower the pressure drop across it and thus the higher is the solvent flux through the membrane. The overall membrane thickness (active layer and porous layer) ranges from about 1 to 10 mils, preferably about 2 to 4 mils. The membrane may be made into supported or freestanding flat sheets, supported or free-standing tubes, or hollow fibers etc. The membranes for the separation of dewaxing solvent from mixtures of dewaxing solvent and dewaxed oil which are the object of the present invention can be fabricated from polyimide polymers preferably aromatic, fully imidized polyimide polymers. The reverse osmosis polyimide membranes can be prepared from a prepolymer solution (e.g. polyamic acid or polyamic acid ester in a solvent), spreading the solvent/polymer solution to form a film and then chemically or thermally imidizing the film to form a membrane. See e.g. U.S.P. 3,546,175, U.S.p. 3,179,632, U.S.p. 3,179,633 and U.S.P. 3,925,211. Alternatively, if the imidized polymer is soluble it can be dissolved in the solvent to form an appropriate casting dope and the membrane cast therefrom. Typical solvents are N,N'-dimethylsulfoxide (DMSO), N,N'-dimethylacetamide (DMAC), hexamethylphosphoramide (HMPA), pyridine, tetramethylurea (TMU), N-methylpyrrolidone (lIMP), N-methyl-2-piperidone, m-cresol} diniethylformamide (DMF) such solvents further being miscible with the membrane immersion or gelation liquid, such immersionZgelation liquid being water, alcohols, dioxane, ketones; preferably, for safety, being water and alcohols; A commercially available polyimide useful for the production of membranes is manufactured and marketed by the Upjohn Company as type 2080 and is sold under that designation in powder form, or under the designation 2080D or 2080DHV in solution form, DMF being the solvent. This material is a highly polar aromatic, fully imidized copolymer derived from the co-condensation of benzophenone-3,-3', 4,4'-tetracarboxylic acid dianhydride (BTDA) and a mixture of dit4-aminophenyl) methane and toluene diamine (or the corresponding diisocyanates, 4 ,41-methylenebis (-phenyl- isocyanate)) and toluene diisocyanate, (MDI and TDI respectively) as described in U. S. Patent No. 3,708,458. The obtained copolyimide has imide linkages which may be represented by the formula: EMI5.1 wherein the copolymer comprises from about 10 to 90% I and 90to 108 II, preferably about 20% I and about 80% II (i.e. 2080). The ratio of polar to nonpolar groups in the respective formula is 3:3 and 3:5. Membranes can be cast from this polymer using the procedure outlined by MSI in U.S.P. 4,307,135. In general the polyimide polymer which can be used to produce membranes which may be useful in the present invention can be represented by the formula EMI5.2 wherein R is a tetravalent radical and R' is a divalent radical, and is preferably an aromatic, fully imidized polymer. Representative polyimide polymers and membrane or film casting techniques which should be useful in preparing membranes suitable for use in the present invention can be found in USP 4,113,628; USP 3,179,623; USP 3,816,303; USP 3,546,175; USP 3,925,211; USP 3,179,633, it being understood that in employing any of the polyimide polymers described, care is exercised by the practitioner in the selection of R and R' and/or in the cross-linking of the polymer to insure that the resulting polyimide polymer membrane is resistant to pressurized ketone. Further, the poly(amide)imides of USP 3,816,303 are contemplated as also being of possible use in the present invention, care again being taken to insure that the polymer membrane is resistant to pressurized ketone. Polyimide polymers such as those polymers produced by- Ciba-Geigy and sold under the designation of XU-2l8 when formed into a membrane have demonstrated some ketone-oil separation capacity but have also been found to be subject to plastic deformation over time in the ketone solvent-dewaxed oil system. Plastic deformation is deemed to indicate that such membranes are unsuitable for use in the present invention. However, such polymers, and others which are not aromatic and/or fully imidized (e.g. USP 4,240,914; Re 30,351; USP 3,822,202) could be subjected to chemical or thermal cross linking and such treatment might possibly render such membranes suitable for use in the present ketoneoil separation process, provided the resulting membrane is not too fragile or too brittle for handling or for exposure to the pressures necessary to practice reverse osmosis. Membranes prepared from the polyimide polymer of USP 4,358,378 having the formula EMI7.1 wherein R is a divalent group may also be used provided the membranes so prepared are not of the large pore ultrafiltration variety described in the patent, but are of the reverse osmosis type. Polyimide membranes can be used immediately as such after preparation. However, they can also be treated with organic solvent to facilitate drying, (if necessary), storage, fabricating into elements and handling. It is well known that polyimides are inherently unstable towards hydrolysis (see Polymer Letters Vol 13, pg. 701-709, 1975) so organic solvent exchange should be practiced to replace aqueous gelation solvent and to prevent membrane deterioration over extended periods of storage, see for example GB 2,073 ,654A, GB 2,051,664A, EP 0023406 or Final Report by Membrane Systems Inc. to Office of Water Research & BR< Technology Development of Chlorine Resistant Membrane, Asymmetric Polyimide Membrane and Porous Substrate, Sudak et al. under contract no. 14-34-0001-9515t Sept. 1980, pp 153-234, pg. 209. Any gelation water can be replaced using any water miscible solvent such as low molecular weight alcohols or ketones, or mixtures thereof and mixtures of alcohols or ketones with glycols or glycerols, e.g. isopropyl alcohol/glycerol; polyethylene glycol, triethylene glycol, MEK, Mink, MEK/MI33K etc. The glycol or glycerol exchanged membrane can then be air dried. Reverse osmosis polyimide membrane useable in the present invention will be able to prevent the passage of a majority of oil molecules having a molecular weight as low as about 300 to 400, and larger. A polyimide membrane will be considered as being of the ultrafiltration type and not a reverse osmosis membrane, for the purposes of the present invention when the membrane no longer retains the bulk of the smallest molecular weight members of the dewaxed oil from the dewaxed oil/ketone solvent mixture being separated as used hereinafter in the specification and the claims. The terms polymide and polyimrde membrane are understood to include all of the above recited polyimide materials, unless a specific polyimide is expressly identified. The polyimide membrane in the form of units or elements can be placed into contact with a dewaxed oil/dewaxing solvent mixture directly, with no conditioning or pretreatment required. This is a distinct operating advantage as compared with the use of a regenerated cellulose membrane as described in European Patent Application Publication tEP 13,834 wherein a pretreatment procedure involving the conditioning of the regenerated cellulose membrane with high pressure alcohol (methanol) followed by high pressure ketone (methyl ethyl ketone) is required. The separation process of the instant invention employing the supported asymmetric polyimide membrane material is conducted by contacting the solvent/oil mixture with the dense side of the Rsymmetric membrane at a temperature of from about -50 to +1500C, preferably about -30 to +100 C, most preferably -20 to about +70 C. The operating pressure must be greater than the osmotic pressure plus any back-pressure in the system. A net driving pressure of from about 100 to 1500 psig preferably about 200 to 600 psig, most preferably about 300 to 500 psig may be typically employed. Any solvent dewaxing process may be employed in the operation of this invention, e.g. indirect heat exchange using, for example, scraped-surface chillers. Other well-known solvent dewaxing processes involve conventional, incremental solvent addition. In this method, solvent is added to the oil at several points along a chilling apparatus. The waxy oil is first chilled with solvent until some wax crystalli zation has occurred and the mixture has thickened considerably. A first increment of solvent is intro duced at this point in order to maintain fluidity, cooling continues and more wax is precipitated. A second increment of solvent is added to maintain flu id- ity. This process is repeated until the desired oil-wax filtration temperature is reached, at which point an additional amount of solvent is added in order to reduce the viscosity of the mixture to that desired for the filtration step. In this method the temperature of the incrementally added solvent should also be about the same as that of the wax/oil/solvent mixture at the point of introduction. If the solvent is introduced at a lower temperature, shock chilling of the slurry occurs resulting in the formation of small and/or acicular shaped wax crystals with attendant poor filter rate. Still another well-known process is the DILCHILLR process wherein a waxy oil is introduced into an elongated, staged cooling zone or tower at a temperature above its cloud point and incrementally introducing a cold dewaxing solvent into said zone, along a plurality of points or stages therein, while maintaining a high degree of agitation so as to effect substantially instantaneous mixing of the solvent and wax/oil mixture as they progress through said zone. The basic concept is shown in U. 5. Patent No. 3,773,650, the disclosures of which are incorporated herein by reference. Common solvents useful for dewaxing waxy petroleum oils may be used in the process of this invention. Representative examples of such solvents are (a) the aliphatic ketones having from 3 to 6 carbon atoms, such as acetone, methyl ethyl ketone (MEK) and methyl isobutyl ketone (MlBK), mixtures of the aforesaid ketones with aroma tics (C6-C9 aromatics) such as benzene, xylene and toluene. In addition, halogenated, low molecular weight hydrocarbons such as the C1-C4 chlorinated hydrocarbons, e.g., dichloromethane, dichloroethane, and mixtures thereof, may be used as sol- vents either alone or in admixture with any of the aforementioned solvents. Further ethers, such as methyl Rsegistered service mark of Exxon Research and Engineering Company. tertiarybutyl ether can also be used alone or in combination with other solvents such as MTBE/toluene. Preferred solvents are MEK/MIBK and MEK/toluene. In the dewaxing of any waxy hydrocarbon oil stock, preferably waxy petroleum oil stock or distillate fraction thereof, more preferably waxy lube oil, transformer oil or fuel oil stocks, the dewaxed oil and the dewaxing solvent may be separated using the process of this invention. In the practice of the separation of dewaxing solvent containing ketone from dewaxed oil the membrane can be employed in the form of bundles of hollow fibers as described in U. S. Patent 3,228,877 or stacks of flat sheets suitably arranged or in the form of a spirally wound membrane element as described in, for example, U.S. Patent 3,417,870, USP 3,173,867, USP 3,367,594, USP 3,386,583, USP 3,397,790. In fabricating such spiral wound elements various adhesives, spacers, backings, seals, etc. are employed. For use in a ketone solvent-dewaxed oil separation process the spiral wound element will typically comprise layers of polyimide membrane wound around a central tube (metal or solvent resistant plastic) containing holes for the permeate, the membrane layers being separated by alternate layers of a permeate carrier such as knitted simple (Dacron, with melamine formaldehyde stiffener) and a feed spacer made of Vexar (a polypropylene mesh). Membrane layers are sealed using an epoxy adhesive to sandwich the permeate cloth into a closed envelope in fluid communication with the perforated central tube leaving the perforations in the central tube as the-only permeate outlet. The epoxy adhesive will generally comprise a ketone resistant resin formulation such as one comprising (') Epon 828 which is a reaction product of bisphenol-A and epichlorohydrin (2) Cabosil MS, (3) Versamid 140 (a polyamide curing agent) (4) Estane 5707F-1 (a polyurethane from B. F. Goodrich) and (5) DMF solvent wherein the components 1/2/3/4/5 are present in typical relationship based on parts by weight of about 100/10/60/4/12, which cures at about 250C over about a 21 day period. This adhesive system is described and claimed in copending application USSN 494,40g. The layers of membrane, permeate carrier and feed spacer are wound around the central tube in a fashion consistent with preparing a spiral wound element. After the element is cured, the ends of the element are trimmed; a nylon seal carrier and a nylon anti-telescoping device are then added. The element is then covered on the outside with an epoxy reinforced fiber glass outer wrap. Elements of any size can be prepared but typical elements are about 8 inches in diameter and about 40 inches long and have ¯ 225 square feet of membrane area and can be used at feed flow rates of about 3û-50 gallons per minute at a 5-15 psi pressure drop. DESCRIPTION OF A SPECIFIC EMBODIMENT Figure 2 describes a specific embodiment of the process of the present invention. Waxy hydrocarbon oil is fed via line (1) into a series of chiller units (2). Dewaxing solvent from storage (3) is fed via lines (4) into the chiller train. As the waxy hydrocarbon oil/solvent mixture progresses through the chiller train it forms a slurry comprising crystals of wax and a mixture of dewaxed oil and dewaxing solvent. This slurry is passed from the chiller train via line (5) to the filter (6). In practice, the chiller train may be a series of scraped surface chillers, or, preferably, a DILCHILL unit as described in U. S. Patent No. 3,773,65û using cold dewaxing solvent, or a combination of DILCHILL chilling and scraped surface chillers, as described in U. S. Patent No. 3,775,288, hereby incorporated by reference. Filter (6) effects the separation of the wax from the slurry thereby forming a wax cake, and a filtrate comprising a mixture of dewaxed oil and dewaxing solvent. The wax is removed from filter (6) via line (7) and sent to further processing. The filtrate is passed via line (8) to at least one membrane unit (9) wherein it contacts, under pressure, the dense side of an asymmetric polyimide membrane at a differential pressure across the membrane ranging from about 100 to 1500 psi. A substantial portion of the dewaxing solvent preferentially permeates through the asymmetric polyimide membrane to form a solvent rich permeate, recovered via line (10) and sent to solvent storage (3) for recycle and an oil rich retentate, recovered via line (11) and sent to separation tower (12) wherein residual solvent is removed from the oil either by means of distillation or stripping. The recovered residual solvent is sent via line (1or) to solvent storage (3) for recycle while the solvent free dewaxed oil is recovered via line (13). While membrane unit (9) shows only one unit, it is to be understood that in practice a multiplicity of units may be used, in parallel and/or in series, and that each unit will contain a multiplicity of membrane elements in series. It is to be understood that the membrane unit may be a spiral wound unit or element, a tubular unit or element, a hollow fiber unit or element, or a plate and frame unit or element. It is also to be understood that in the above representation, pumps, valves and assorted hardware have been omitted for the sake of simplicity, their placement in practice being within the scope of those skilled in the art. EXPERIMENTAL Samples of polyimide membrane were evaluated in a high pressure, round membrane test cell. The membranes were cut into 3O inch diameter circles and placed in a test cell having a 2.6 inch opening. The membrane samples are sealed to the high pressure side of the cell by the use of a teflon O-ring. The membrane samples are supported on a intered stainless steel disk. The test cells are connected into a recirculating loop wherein mixture of dewaxed oil/dewaxing solvent or pure solvent are contacted with the skin side of the membrane to be tested. Within the test cell the mixture is passed over the surface of the membrane at a rate of about 22.3 cm3/sec, a rate great enough to prevent or minimize any concentration polarization effect. All membrane samples were tested under the following conditions unless otherwise indicated: pressure was 400 psig, temperature was 25 C, in a feed mixture consisting of 30 wt.% dewaxed oil (150 N), 35 wit.% MEK and 35 wt.% MIBK. (MEK/tSIBE 1:1). All solvent permeation rates are expressed in liters per square meter of membrane per 24 hour day (lZm2-d). EXAMPLE 1 Samples of polyimide membranes were secured from Membrane Systems Inc. (MSI) and treated in accordance with the procedure, and gave the test results presented in Table 1. Except where otherwise indicated, the membranes were tested for the separation of ketone dewaxing solvent (1:1 MEK/MIBK) from dewaxed oil and also compared with membranes of regenerated cellulose (R.C.). The R.C. membranes (and, -when indicated, some of the polyimide membranes) were preconditioned to pass ketone by the procedure of EP 13,834 (the R.C. membranes were first water washed then successively permeated with methanol and MEK at 400 psig at room temperature) but, in the case of polyimide membrane such pretreatment is not necessary. The polyimide membrane samples secured from MSI are believed to have been prepared using Upjohn 2080 polyimide polymer by the technique described in USP 4,307,135, which method is taught as yielding membranes reportedly possessing good salt rejection and water permeability. The details of the exact procedure employed to produce each membrane sample tested below is not known. It is to be noted that in a few instances (see samples 3-6, 26, 31) the results were obtained on a system which employed only MEK as solvent. Runs 32-37 demonstrate that membranes (26-31) which showed rather high flux rates on an oil single solvent system (MEK) showed a dramatic reduction in flux rate when tested on the oil-mixed solvent system (MEK/MIBR). The data does clearly demonstrate that polyimide membranes do separate dewaxing solvent containing ketone from dewaxed oil with good selectivity. Table 1 Solvent Oil Pretreatment Permeation Rejection Sample Procedure Rate (1/mê-d) (%) (A) 1B,C air dry 77 99.33 2B,C air dry 90 98.33 3C*,D Solvent Exchange 50:50 H2O:IPA (30 min) then 50:50 acetone: IPA (30 min) 633 98.0 Then Dried (#10 min) 4C*D ( " ) 776 85.0 3C*D ( " ) 1000 90.0 6C*D ( " ) 971 97.5 7C air dried (18 hr) 48.4 # 7.2 95.2 # 3.9 8C wet/dried in situ 358.6 # 53.8 98.8 # 0.7 9Ú 5% glycerol in water/air dry 197.2 # 16.1 94.6 # 4.5 10Ú,C 10% glycerol in water/air dry 278 # 28.7 99.6 # 0.1 11Ú,C 15% glycerol in water/air dry 276.1 # 30.5 99.6 # 0.06 (43 hr.) 12Ú,C 20% glycerol in water/air dry 439.3 # 28.7 98.8 # 0.7 (43 hr.) 13Ú,C 25% glycerol in water/air dry 426.7 # 66.3 99.5 # 0.1 14Ú,C 30% glycerol in water/air dry 396.2 # 30.5 99.5 # 0.1 11C 15% glycerol in water/43 hr dry 276.1 # 30.5 99.6 # 0.06 15C 15% glycerol in water/140 hr dry 380.1 # 35.9 99.0 # 0.6 12C 20% glycerol in water/43 hr dry 439.3 # 28.7 98.8 # 0.7 16C 20% glycerol in water/140 hr dry 392.7 # 84.3 98.6 # 0.7 Table 1 Continued Solvent Oil Pretreatment Permeation Rejection Sample Procedure Rate (1/mê-d) (%) (A) 17 Permeation at 400 psi: Methanol - MEK 273 # 26.7 95.7 # 2.1 18 MEK 547 # 103 93 # 4.1 19 No pretreatment 471 # 28.5 93 # 3 20 Membranes dried from 15% glycerol in methanol - stored 5 days then permeated at 400 psi - Methanol then MEK 184 # 7 98.7 # 0.5 21 permeated at 400 psi MEK 326 # 21.4 94.9 # 3.5 22 no pretreatment 225 # 5.3 94 # 3 23C Regenerated cellulose 571 70 24C PM 100 R. C. (10 thick) used wet 867.8 # 52 49 # 9 25C PM 250 R. C. (17.5 ) used wet 435.7 # 34.1 64.6 # 2.0 26E,F 25% formamide in MeOH (15 min) air dry (15 min) 986 97.17 27E,F ( " ) 520 77.50 28E,F ( " ) 520 91.47 29E,F ( " ) 484 95.04 30E,F ( " ) 487 95.04 31E,F ( " ) 843 98.97 Solvent Oil Pretrteatment Permeation Rejection Sample Procedure Rate (1/mê-d) (%) (A) 32F,G Membrane 26 after 150N/MEK (above) 407 93.2 33F,G Membrane 27 after 150N/MEK (above) 274 68.0 34F,G Membrane 28 after 150N/MEK (above) 305 87.1 35F,G Membrane 29 after 150N/MEK (above) 233 90.5 36F,G Membrane 30 after 150N/MEK (above) 264 84.4 37F,G Membrane 31 after 150N/MEK (above) 389 98.6 A. Oil rejection = Feed Oil Conc. - Permeate Oil Conc X100% Feed Oil Conc. B. Membrane cannot be air dried without a permanent loss of solvent flux. C. Membrane was pressure permeated sequentially by methanol then MEK at 400 psi ambient temperature before being tested for ketone/oil separation. C* Samples 3-6 were pressure sequentially by methanol then MEK at 400 psi for about 20 minutes each, ambient temperature before being tested for ketone/oil separation. D. Permeation test conducted on 20% 150N in MEK at 400 psi, ambient temperature E. Permeation test conducted on 30% 150N in MEK at 400 psi, ambient temperature F. Membranes stored in water prior to use, had a rotten egg odor indicating possible membrane deterioration. G. Permeation test conducted on 30% 150N in MEK/MIBK 1:1 at 400 psi, ambient temperature. 1. All dried membrane were air dried at least 18 hrs after being immersed for 15 minutes in the aqueous glycerol solutions. Example 2 Ciba Geigy XU-218 polyimide a polymer based on 5(6)-amino-1-(4'-aminophenyl)-1, 3, 3-trimethylindane was evaluated as a membrane for the ketone/oil separation process. A 20 wt.% solution of XU 218 in a 4:1 ratio solvent of dioxane/DMF was hand cast using a doctor blade with an 11 mil gap and an 8 sec. solvent evaporation time. The membrane was gel led in tap water. The membrane is initially insoluble in MEK, MIBK and acetone. The membrane was determined to be insoluble in an unpressurized hot mixture of 30 wt% 150N oil in 1:1 MEK/MISK. A test run was conducted using the ketone oil solution at 400 psig at ambient temperatures. Three test circles were evaluated which gave an average permeate flux of 1238 + 187 1/m2-d and an oil rejection of 71.5 + 6%. The test circles were examined after use and were found to have wrinkled. This membrane is plasticized by exposure to the feed and deforms under pressure and as presently constituted is thus unsuitable for use in the present system. Example 3 General Electric Ultem 1000 polyetherimide polymer was also treated to determine its suitability for use in this separation. It is believed the polymer has the probable structure: EMI19.1 see USP 4,156,547 and 4,073,773. A series of casting solutions was prepared. Nineteen wt.% polymer was mixed into solutions of 0:1; 1:3 and 1:1 dioxane/DMF. Casting was by hand using a doctor blade with a 10 mil gap. An evaporation time of 8-10 seconds and a water gel bath were used. Membrane thicknesses were: 0:1 4.0 mils + 0.3 1:3 3.1 mils + 0.2 1:1 3.1 mils + 0.2 The membranes were evaluated for ketone/oil separation capability on a solution of 30% 150N oil in 1:1 MEK/MlBK. Test conditions were: Pressure - 400 psi; Temp - ambient. Membrane performance is as below: Oil Membrane Flux (l/m2-d) Rejection 96 0:1 2090 + 370 13.0 + 4 1:3 2279 + 150 33.6 + 1 1:1 1120 + 150 60.8 + 7 The membranes were seen to undergo plastic deformation under the test conditions. The polymer membrane also plasticized in MEK at room temperature. The membrane is not suitable for ketone/oil separation. In this patent specification inches = 2.54 Cm mil = 10-3inch = 2.54 x 10-5m foot = 30.48 cm square foot = 929 cm2 psi = 6.895 kPa psig = 6.895 kPa gauge pressure inch Hg = 3.377 kPa gallon (U.S) = 3.785 litre micron and p = 1 x 10- X USP stands for U.S.Patent Re stands for U.S. Patent Re-issue &num; stands for number "Teflon" is a registered Trade Mark. The adhesive system described and claimed in copending USSN 494,409 referred to supra is described and claimed in our European Patent Application No. filed on or about the same date as the present application under the title "Adhesive System for the Production of Spiral Wound Membrane Elements for Use in Organic Fluid Mixture Separations" (inventors : William M. King and William W. Wight).

Claims: CLAIMS 1. The solvent dewaxing of waxy hydrocarbon oils wherein the waxy oil is contacted with a dewaxing solvent cooled to precipitate the wax to yield a wax-oil-solvent slurry and wherein the slurry is separated into a wax stream and a solvent/oil stream and wherein the solventloil stream is separated into a solvent stream and an oil stream, wherein at least part of the solvent oil separation is conducted under reverse osmosis conditions using a selective permeation barrier which is an permeable asymmetric polyimide membrane. 2. The process of claim 1 wherein the solvenvoil stream to be separated is contacted with the dense side of the asymmetric polyimide membrane, which polyimide membrane is made from an aromatic, fully imidized polyimide. 3. The process of claim 1 or claim 2 wherein the solvent recovered by means of the asymmetric polyimide membrane is recycled to the waxy hydrocarbon oil dewaxing process. 4. The process of any one of claims 1 to 3 wherein the dewaxing solvent is selected from the groups consisting of aliphatic ketones having from 3 to 6 carbons, aromatic hydrocarbons, halogenated low molecular weight hydrocarbons and mixtures thereof. 5. The process of any one of claims 1 to 4 wherein the dewaxing solvent is a mixture of methyl ethyl ketone and methyl isobutyl ketone. 6. The process of any one of claims 1 to 4 wherein the dewaxing solvent is a mixture of methyl ethyl ketone and toluene. 7. The process of any one of claims 1 to 6 wherein the waxy hydrocarbon oil is a waxy petroleum oil. 8. The process of any one of claims 1 to 7 wherein the waxy hydrocarbon oil is a waxy lubricating oil stock. 9. The process of any one of claims 1 to 8 wherein the permeable asymmetric polyimide membrane is in the form of a spiral wound element.

Inventors: WIGHT, WILLIAM WALLACE
Applicants: EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1984
Main classification: C10G73
IPC codes: B01D71, C10G73