HIGH PURITY PARAFFINIC SOLVENT COMPOSITIONS, AND PROCESS FOR THEIR MANUFACTURE

Abstract: Discloses high purity solvent compositions constituted of n-paraffins and isoparaffins, with the isoparaffins containing predominantly methyl branches, and having an isoparaffin:n-paraffin ratio sufficient to provide superior low temperature properties and low viscosities. The solvent compositions are made by a process wherein a waxy, or long chain paraffinic feed, especially a Fischer-Tropsch wax, is reacted over a dual function catalyst to produce hydroisomerization and hydrocracking reactions at 700 DEG F+ conversion levels ranging from about 20 to 90 wt.% to provide a C5-1050 DEG F crude fraction. The C5-1050 DEG F crude fraction is then topped via atmospheric distillation to produce a low boiling fraction with an upper end point boiling between about 650 DEG F and 750 DEG F. The low boiling fraction is fractionated and a narrow boiling range solvent obtained therefrom; one which can be further divided into solvent grades of various boiling ranges.

Description: HIGH PURITY PARAFFINIC SOLVENT COMPOSITIONS, AND PROCESS FOR THEIR MANUFACTURE 1. Field of the Invention This invention relates to high purity paraffinic solvent compositions, and process for the production of such compositions by the hydroisomerization and hydrocracking of long chain linear paraffins, especially Fischer-Tropsch waxes. In particular, it relates to solvent compositions characterized as mixtures of -Cjo n-paraffins and isoparaff s, with the isoparaffms containing predominantly methyl branching and an isoparaffin:n-paraffιn ratio sufficient to provide superior low temperature properties and low viscosities. 2. Background Paraffinic solvents provide a variety of industrial uses. For example, NORPAR solvents, several grades of which are marketed by Exxon Chemical Company, e.g. , are constituted almost entirely of C :0 -C linear, or normal paraffins (n-paraffins). They are made by the molecular sieve extraction of kerosene via the ENSORB process. These solvents, because of their high selective solvency, low reactivity, mild odor and relatively low viscosity, are used in aluminum rolling oils, as diluent solvents in carbonless copy paper, and in spark erosion machinery. They are used successfully in pesticides, both in emulsifiable concentrates and in formulations to be applied by controlled droplet application, and can even meet certain FDA requirements for use in food-related applications. The NORPAR solvents, while having relatively low viscosity, unfortunately have relatively high pour points; properties which cannot be improved in the ENSORB process by a wider n-paraffin cut because the C 1 S + n-paraffins have high melting points. Thus, the addition of C,, +- paraffins will only worsen the pour point. Solvents constituted of mixtures of highly branched paraffins, or isoparaffms, with very low n-paraffin content, are also commercially available. For example, several grades of ISOPAR solvents, i.e. , iso¬ paraffms or highly branched paraffins, are supplied by Exxon Chemical Company. These solvents, derived from alkylate bottoms (typically prepared by alkylation), have many good properties; e.g. , high punty, low odor, good oxidation stability, low pour point, and are suitable for many food- related uses. Moreover, they possess excellent low temperature properties. Unfortunately however, the ISOPAR solvents have very high viscosities, e.g. , as contrasted with the NORPAR solvents. Despite the need, a solvent which possesses substantially the desirable properties ot both the NORPAR and ISOPAR solvents, but particularly the low viscosity ot the NORPAR solvents and the low temperature properties of the ISOPAR solvents is not available 3. Summary of the Invention The present invention accordingly, to meet these and other needs, relates to a high purity solvent composition comprising a mixture of paraffins having from about 8 to about 20 carbon atoms, i.e. , G,-C 20 , preferably from about C l0 -C !ft , carbon atoms, in the molecule. The solvent composition has an isoparaffin- n-paraffin ratio ranging from about 0 5 1 to about 9: 1 , preferably from about 1: 1 to about 4 1 The isoparaffms of the mixture contain greater than fifty percent, 50% , mono-methyl species, e.g. , 2-methyl, 3-methyl, 4-methyl, > 5- methyl or the like, with minimum formation of branches with substituent groups of carbon number greater than 1 , i.e. , ethyl, propyl, butyl or the like, based on the total weight of isoparaffms in the mixture Preterably, the isoparaffms of the mixture contain greater than 70 percent of the mono-methyl species, based on the total weight of the isoparaffms in the mixture. The paraffinic solvent mixture boils within a range of from about 320°F to about 650°F, and preferably within a range of from about 350°F to about 550°F In preparing the different solvent grades, the paraffinic solvent mixture is generally fractionated into cuts having narrow boiling ranges, i.e., 100°F, or 50°F boiling ranges. The properties of these solvents, e g , viscosity, solvency and density, are similar to NORPAR solvents of similar volatility but have significantly lower pour points These solvents also have significantly lower viscosities than ISOPAR solvents of similar volatility In tact, these solvents combine many of the most desirable properties found in the NORPAR and ISOPAR solvents In particular however, the solvents of this invention have the good low temperature properties of ISOPAR solvents and the low viscosities of the NORPAR solvents; and yet maintain most of the other important properties of these solvents. The solvents of this invention are produced by the hydrocracking and hydroisomerization of + paraffinic, or waxy hydrocarbon feeds, especially Fischer-Tropsch waxes, or reaction products, at least a fraction ot which boils above 700°F, i.e. , at 700°F-t- The waxy feed is first contacted, with hydrogen, over a dual functional catalyst to produce hydroisomerization and hydrocracking reactions sufficient to convert at least about 20 percent to about 90 percent, preferably from about 30 percent to about 80 percent, on a once through basis based on the weight of the 700°F+ feed component, or 700°F + feed, to 700°F- materials, and produce a liquid product boiling at trom about 74°F to about 1050°F, i.e. , a C 5 -1050°F liquid product, or crude fraction. The C S - 1050°F crude traction is topped via atmospheric distillation to produce two fractions, (I) a low boiling fraction having an initial boiling point ranging between about 74 °F and about 100°F, and an upper end boiling point ranging between about 650°F and about 750°F, preferably between about 650°F and 700°F, and (ii) a high boiling fraction having an initial boiling point ranging between about 650°F and about 750°F, preferably from about 650°F and 700°F, and an upper end boiling point of about 1050°F, or higher, i.e. , 1050°F + . This high boiling fraction typically constitutes a lube fraction. The solvent of this invention is recovered from the low boiling fraction, or fraction boiling between about C 5 and about 650°F to 750°F. The solvent on recovery from the low boiling fraction is fractionated into several narrow boiling range grades of solvent, preferably solvents boiling over a 100°F, and preferably a 50° F range. 4. Detailed Description The feed materials that are hydroisomeπzed and hydrocracked to produce the solvents of this invention are waxy feeds, i.e., C 5 + , preferably boiling above about 350°F (1 17°C), more preferably above about 550°F (288°C), and are preferably obtained from a Fischer-Tropsch process which produces substantially normal paraffins, or may be obtained from slack waxes. Slack waxes are the by-products of dewaxing operations where a diluent such as propane or a ketone (e.g. , methylethyl ketone, methyl isobutyl ketone) or other diluent is employed to promote wax crystal growth, the wax being removed from the lubricating oil base stock by filtration or other suitable means. The slack waxes are generally paraffinic in nature, boil above about 600°F (316°C), preferably in the range of 600°F (316°C) to about 1050°F (566°C), and may contain from about 1 to about 35 wt. % oil. Waxes with low oil contents, e.g. , 5-20 wt. % are preferred; however, waxy distillates or raffinates containing 5-45 % wax may also be used as feeds. Slack waxes are usually freed of polynuclear aromatics and hetero-atom compounds by techniques known m the art; e.g. , mild hydrotreating as descnbed in U.S. Patent No 4,900,707, which also reduces sulfur and nitrogen levels preferably to less than 5 ppm and less than 2 ppm, respectively Fischer-Tropsch waxes are preferred teed materials, having negligible amounts of aromatics, sulfur and nitrogen compounds. The Fischer-Tropsch liquid, and wax, is characterized as the product of a Fischer- Tropsch process wherein a synthetic gas, or mixture of hydrogen and carbon monoxide, is processed at elevated temperature over a supported catalyst compnsed of a Group VIII metal, or metals, of the Penodic Table of The Elements (Sargent-Welch Scientific Company, Copyright 1968), e g , cobalt, ruthenium, iron, etc The Fischer-Tropsch liquid contains C s + , preterably C 10 + , more preferably d u + paraffins A distillation showing the tractional make up (± 10 wt. % for each traction) ot a typical Fischer-Tropsch process feedstock is as follows: Boiling Temperature Range Wt % of Fraction IBP - 320°F 13 320 - 500°F 23 500 - 700°F 19 700 - 1050°F 34 1050°F+ _L 100 The wax feed is contacted, with hydrogen, at hydrocracking/ hydroisomenzation conditions over a bifunctional catalyst, or catalyst containing a metal, or metals, hydrogenation component and an acidic oxide support component active in producing both hydrocracking and hydroisomerzation reactions. Preterably, a fixed bed of the catalyst is contacted with the teed at conditions which convert about 20 to 90 wt. % , preferably about 30 to 80 wt. % of the 700°F-t- feed components (or a 700°F + feed) to a low boiling fraction having an initial boiling point of about C 5 (about 74°F to about 100°F) and an end boiling point ranging between about 650°F and about 750°F, preferably between about 650°F and about 700°F, and a higher boiling fraction having an initial boiling point corresponding to the upper end boiling point of the low boiling fraction and a higher end boiling point of 1050°F, or greater. In general, the hydrocracking/hydroisomerization reaction is conducted by contacting the waxy feed over the catalyst at a controlled combination of conditions which produce these levels of conversion, e.g. , by selection of temperatures ranging from about 400°F to about 850°F, preferably from about 500°F to about 700°F, pressures ranging generally from about 100 pounds per square inch gauge (psig) to about 1500 psig, preferably from about 300 psig to about 1000 psig, hydrogen treat gas rates ranging from about 1000 SCFB to about 10,000 SCFB, preferably from about 2000 SCFB to about 5000 SCFB, and space velocities ranging generally from about 0.5 LHSV to about 10 LHSV, preferably from about 0.5 LHSV to about 2 LHSV. The active metal component of the catalyst is preferably a Group VIII metal, or metals, of the Periodic Table Of The Elements (Sargent-Welch Scientific Company Copyright 1968) in amount sufficient to be catalytically active for hydrocracking and hydroisomerization of the waxy feed. The catalyst may also contain, in addition to the Group VIII metal, or metals, a Group IB and/or a Group VIB metal, or metals, of the Periodic Table. Generally, metal concentrations range from about 0.05 percent to about 20 percent, based on the total weight of the catalyst (wt. %), preferably from about 0.1 wt. percent to about 10 wt. percent. Exemplary of such metals are such non-noble Group VIII metals as nickel and cobalt, or mixtures of these metals with each other or with other metals, such as copper, a Group IB metal, or molybdenum, a Group VIB metal. Palladium and platinum are exemplary of suitable Group VIII noble metals The metal, or metals, is incorporated with the support component of the catalyst by known methods, e.g. , by impregnation of the support with a solution of a suitable salt or acid of the metal, or metals, drying and calcination. The catalyst support is constituted of metal oxide, or metal oxides, components at least one component of which is an acidic oxide active in producing olefin cracking and hydroisomerization reactions Exemplary oxides include silica, silica-alumina, clays, e g , pillared clays, magnesia, titania, zirconia, hahdes, e.g. , chlonded alumina, and the like The catalyst support is preferably constituted of silica and alumina, a particularly preferred support being constituted of up to about 35 wt. % silica, preferably from about 2 wt. % to about 35 wt. % silica, and having the following pore- structural characteristics: Pore Radius. A Pore Volume 0-300 > 0.03 ml/g 100-75,000 < 0.35 ml/g 0-30 < 25 % of the volume of the pores with 0-300 A radius 100-300 < 40% of the volume of the pores with 0-300 A radius The base silica and alumina matenals can be, e.g , soluble silica containing compounds such as alkaii metal silicates (preferably where Na 3 O:SιO 2 = 1 :2 to 1 :4), tetraalkoxy silane, orthosi c acid ester, etc , sulfates, nitrates, or chlondes of aluminum alkaii metal aluminates, or inorganic or organic salts of aJkoxides or the like. When precipitating the hydrates of silica or alumina from a solution of such starting materials, a suitable acid or base is added and the pH is set within a range of about 6.0 to 1 1.0. Precipitation and aging are earned out, with heating, by adding an acid or base under reflux to prevent evaporation of the treating liquid and change of pH The remainder of the support producing process is the same as those commonly employed, including filtering, drying and calcination of the support mateπal The support may also contain small amounts, e.g. , 1 -30 wt % , of matenals such as magnesia, titania, zirco a, hafnia, or the like. Support materials and their preparation are descnbed more fully in U.S Patent No 3,843,509 incorporated herein by reference The support materials generally have a surface area ranging from about 180-400 m /g, preferably 230-375 m 2 /g, a pore volume generally of about 0.3 to 1 0 ml/g, preferably about 0.5 to 0.95 ml/g, bulk density of generally about 0.5- 1.0 g/ml, and a side crushing strength of about 0 8 to 3.5 kg/mm The hydrocracking/hydroisomenzation reaction is conducted in one or a plurality of reactors connected in series, generally from about 1 to about 5 reactors; but preferably the reaction is conducted in a single reactor. The waxy hydrocarbon feed, e.g. , Fischer-Tropsch wax, preferably one boiling above about 350°F ( 177°C), more preferably above about 550°F (288°C), is fed, with hydrogen, into the reactor, a first reactor of the senes, to contact a fixed bed of the catalyst at hydrocracking/hydroisomenzation reaction conditions to hydrocrack, hydroisomenze and convert at least a portion of the waxy feed to products suitable as solvents for the practice of this invention. The following examples are illustrative of the more salient features of this invention. All parts, and percentages, are given in terms of weight unless otherwise specified. Examples 1 -3 A mixture of hydrogen and carbon monoxide synthesis gas (H 2 :CO 2. 1 1-2. 16) was converted to heavy paraffins in a slurry Fischer- Tropsch reactor. A titania supported cobalt rhenium catalyst was utilized for the Fischer-Tropsch reaction. The reaction was conducted at 422-428°F, 287-289 psig, and the feed was introduced at a linear velocity of 12 to 17.5 cm/sec. The alpha of the Fischer-Tropsch synthesis step was 0.92. The paraffinic Fischer-Tropsch product was isolated in three nominally different boiling streams; separated by utilizing a rough flash. The three boiling fractions which were obtained were: 1 ) a C -500°F boiling fraction, i.e. , F- T cold separator liquids; 2) a 500-700°F boiling fraction, i.e. , F-T hot separator liquids; and 3) a 700 C F+ boiling fraction, i.e. , an F-T reactor wax. The 700 o F+ boiling fraction, or reactor wax, was then hydroisomeπzed and hydrocracked over a Pd/silica-alumina catalyst (0.50 wt. % Pd; 38 wt. % A O,; 62 wt. % SiO : ), at process conditions providing a 39.4 wt. % conversion of the 700°F - materials to 700°F- materials. The operating conditions, wt. % yield, and product distributions obtained in the run are as described in Table 1. Table 1 Operating Conditions Temp. , °F 638 LHSV, v/v/h 1.2 PSIG 71 1 H 2 Treat rate, SCF/B 2100 Yields, wt. % C,-C 4 0.97 C S -320°F 10.27 320-500°F 14 91 500-700°F 29.99 700° F+ 43.86 Total 100.00 700°F+ Conversion, wt. % 39.4 15/5 Distillation Yields, wt. % IBP-650°F 50.76 650°F+ 49.24 The total liquid product from this run was first topped at 650°F in an atmospheric 15/5 distillation. The low boiling, or 650°F- fraction was then fractionated into ten ( 10) LV% cuts in a 15/5 distillation, 30 LV (Liquid Volume) % of which constituted the solvent of this invention. The physical properties of three of these cuts, representing the 30-40 LV% , the 40-50 LV % , and 50-60 LV % cuts, respectively, are listed in Tabie 2 as Sample Nos. 1 , 2 and 3, respectively. Table 2 A list of the normal paraffin content by G.C. , and branching density by NMR, % carbon, for each of the three cuts, representative of three solvent grades, is given in Tables 3 and 4, respectively. Table 3 NORMAL PARAFFIN CONTENT BY GC Table 4 BRANCHING DENSITY BY NMR, % CARBON NM = Not Measured Comparison of the physical properties of the solvents of this invention, by grade, shows that they compare favorably with, and in some respects are superior to NORPAR and ISOPAR solvents. The solvents of this invention, albeit structurally different from the ISOPAR solvents which are highly branched, with low paraffin content, like the ISOPARs have low odor, good selective solvency, high oxidative stability, low electrical conductivity, low skin irritation and suitability for many food-related uses. Unlike the ISOPAR solvents however, the solvents of this invention have low viscosities. Moreover, though structurally different from the NORPAR solvents which are essentially all n-paraffins, the solvents of this invention like the NORPAR solvents have low reactivity, selective solvency, moderate volatility, relatively low viscosity and mild odor. Unlike the NORPAR solvents however, the solvents of this invention have low pour points. The solvents of this invention thus have most of the desirable features of both the NORPAR and ISOPAR solvents, but are superior to the NORPAR solvents in that they have pour points ranging from about -20°F to about -70°F, while the pour points of the NORPAR solvents range from about 45 °F to about -6°F; and are superior. to the ISOPAR solvents in that they have viscosities at 25°C ranging from about 1.82 cSt to about 3.52 cSt, while the viscosities of the ISOPAR solvents range from about 2.09 cSt to about 9. 17 cSt. The unique properties of the solvents of this invention, provide advantages in a variety of current solvent and fluids applications, e.g. , aluminum rolling, secondary PVC plasticizers and inks. In addition, mild hydrotreatment of these solvents produces a material which readily passes the "readily carbonizable substance test" (i.e. , hot acid test) which makes the solvents applicable to a wide variety of medicinal and food applications. It is apparent that vanous modifications and changes can be made without departing the spirit and scope of this invention.

Claims: CLAIMS: 1. A high purity solvent composition which comprises a mixture of paraffins of carbon number ranging from about Cs to about C20, has a molar ratio of isoparaffinsrn-paraffins ranging from about 0.5: 1 to about 9:1 and the isoparaffins of the mixture contain greater than 50 percent of the mono-methyl species, based on the total weight of the isoparaffms of the mixture. 2. The composition of claim 1 wherein the mixture of paraffins has a carbon number ranging from about to about 3. The composition of claim 1 wherein the mixture contains greater than 70 percent of the mono-methyl species. 4. The composition of claim 1 wherein the solvent mixture boils at a temperature ranging from about 320°F to about 650°F. 5. The composition of claim 4 wherein the solvent mixture boils within a range of from about 350°F to about 550°F. 6. The composition of claim 4 wherein the solvent is comprised of a mixture of paraffins of carbon number ranging from about C 1 0 to about C 16. 7. The composition of claim 1 wherein the solvent mixture is of carbon number ranging from about Cι 0 -Cι 6 , the mixture contains greater than 70 percent of the mono-methyl species and boils within a range of from about 350°F to about 550°F. 8. The composition of claim 1 wherein the paraffinic mixture has a molar ratio of isoparaffins:n-paraffins ranging from about 1 : 1 to about 4: 1. 9. A process for the production of a high purity solvent composition as described by any of claims 1 through 8, which comprises contacting a C5+ paraffinic feed, with hydrogen, over a dual functional catalyst to produce hydroisomerization and hydrocracking reactions and 700°F+ conversion levels ranging from about 20 percent to about 90 percent on a once through basis based on the weight of total feed, to produce a crude fraction boiling between about C5 and 1050°F, topping said crude fraction by atmospheric distillation to produce a low boiling fraction having an upper end boiling point between about 650°F and about 750°F, and recovering from the low boiling fraction said high purity solvent composition. 10. The process of claim 9 wherein the high purity solvent composition that is recovered is characterized as a mixture of paraffins which has a carbon number ranging from about C10 to about C \ .

Inventors: RYAN DANIEL FRANCIS, SILVERBERG STEVEN EARL, WITTENBRINK ROBERT JAY, RYAN, DANIEL, FRANCIS, SILVERBERG, STEVEN, EARL, WITTENBRINK, ROBERT, JAY
Applicants: EXXON RESEARCH ENGINEERING CO, EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1996
Main classification: C10G45
IPC codes: C07C5, C07C9, C10G2, C10G35, C10G45, C10G47