PROCESS FOR PREPARING AN ETHER

Abstract: An olefin is reacted with an alcohol to provide an ether or mixture of ethers employing as a catalyst a zeolite having X-ray diffraction lines of table (I).

Description: PROCESS FOR PREPARING AN ETHER This invention relates to a process for preparing an ether by the catalytic reaction of an olefin with an alcohol. Zeolitic materials, both natural and synthetic, have been demonstrated in the past to have catalytic properties for various types of organic conversion reactions. Certain zeolitic materials are ordered, porous crystalline aluminosilicates having a definite crystalline structure as determined by X-ray diffraction, within which there are a large number of smaller cavities which may be interconnected by a number of still smaller channels or pores. These cavities and pores are uniform in size within a specific :eolitic material. Since the dimensions of these pores are such as to accept for adsorption molecules of certain dimensions while rejecting those of larger dimensions, these materials have come to be known as "molecular sieves" and are utilized in a variety of ways to take advantage of these properties. Such molecular sieves, both natural and synthetic, include a wide variety of positive ion-containing crystalline silicates. These silicates can be described as a rigid three-dimensional framework of SiO, and Periodic Table Group IIIA element oxide, e.g., A10,, in which the tetrahedra are cross-linked by the sharing of oxygen atoms whereby the ratio of the total Group IIIA element, e.g., aluminum, and silicon atoms to oxygen atoms is 1:2. The electrovalence of the tetrahedra containing the Group IIIA element, e.g., aluminum, is balanced by the inclusion in the crystal of a cation, e.g., an alkali metal or an alkaline earth metal cation. This can be expressed wherein the ratio of the Group IIA element, e.g., aluminum, to the number of various cations, such as Ca/2, Sr/2, Na, or Li, is equal to unity. One type of cation may be exchanged either entirely or partially with another type of cation utilizing ion exchange techniques in a conventional manner. By means of such cation exchange, it has been possible to vary the properties of a given silicate by suitable selection of the cation. Prior art techniques have resulted in the formation of a great variety of synthetic zeolites. Many of these zeolites have come to be designated by letter or other convenient symbols, as illustrated by zeolite Z (U.S. Patent No. 2,882,243), zeolite X (U.S. Patent No. 2,882,244), zeolite Y (U.S. Patent No. 5,130,007), zeolite 2K-5 (U.S. Patent No. 3,247,195), zeolite ΣK-4 (U.S. Patent No. 3,314,752), zeolite ZSM-5 (U.S. Patent No. 3,702,886), zeolite ZSM-11 (U.S. Patent No. 3,709,979), zeolite ZSM-12 (U.S. Patent No. 3,832,449), zeolite ZSM-20 (U.S. Patent No. 3,972,983), zeolite ZSM-33 (U.S. Patent No. 4,016,243), and zeolite ZSM-25 (U.S. Patent No. 4,076,842). The SiO-,/Al-0- ratio of a given zeolite is often variable. For example, zeolite X can be synthesized with SiO-j/Al-O, ratios of from 2 to 3; zeolite Y, from 5 to 6. In some zeolites, the upper limit of the SiO^/A^O^ ratio is unbounded. ZSM-5 is one such example wherein the Si0~/Al 7 0, ratio is at least 5 and up to the limits of present analytical measurement techniques. U.S. Patent No. 3,941,871 (Re. 29,948) discloses a porous crystalline silicate made from a reaction mixture containing no deliberately added alumina in the recipe and exhibiting the X-ray diffraction pattern characteristic of ZSM-5. U.S. Patent Nos. 4,061,724, 4,073,865 and 4,104,294 describe crystalline silicates of varying alumina and metal content. There is a need for an efficient catalytic process to manufacture ethers by the reaction of light ole ins with lower alkanols augmenting the supply of high octane blending stocks for gasoline. Relatively low molecular weight ethers such as methyl-t-butyl ether (MTBE) and t-amyl methyl ether (TAME) are in the gasoline boiling range and are known to have a high blending octane number. The petrochemicals industry produces mixtures of light olefin streams in the C 2 to C- molecular weight range and the conversion of such streams, or fractions thereof, to ethers can provide products useful as blending stocks for gasoline and also as solvents. Various catalytic processes have already been proposed for the reaction of light olefins with lower alkanols to provide ethers. According to U.S. Patent No. 4,042,653, diisopropylether (DIPE) can be prepared from isopropyl alcohol (IPA) employing a montmorillonite clay catalyst, optionally in the presence of added propylene. U.S. Patent No. 4,175,210 discloses the use of silicatungstic acid as catalyst for the reaction of olefin(s) with alcohol(s) to provide ether(s). As disclosed in U.S. Patent No. 4,182,914, DIPE is produced from IPA and propylene in a series of operations employing a strongly acidic cation exchange resin as catalyst. U.S. Patent No. 4,418,219 describes the preparation of MTBE by reacting isobutylene and methanol in the presence of boron phosphate, blue tungsten oxide or crystalline aluminosilicate zeolite having a silica to alumina mole ratio of at least 12:1 and a constraint index of from 1 to 12 as catalyst. U.S. Patent No. 4,605,787 discloses the preparation of alkyl tert-alkyl ethers such as MTBE and TAME by the reaction of a primary alcohol with an olefin having a double bond on a tertiary carbon atom employing as catalyst an acidic zeolite having a constraint index of from 1 to 12, e.g., zeolite ZSM-5, 11, 12, 25, dealuminized zeolite Y and rare earth-exchanged zeolite Y. European Patent Publication No. 55,045 describes a process for reacting an olefin and an alcohol to provide an ether, e.g., isobutene and methanol to provide MTBE, in the presence of an acidic zeolite such as zeolite Beta, zeolites ZSM-5, 8, 11, 12, 25, 55, 43 and 48, and others, as catalyst. The present invention resides in a process for producing an ether or mixture of ethers which comprises reacting at least one olefin with at least one alcohol under etherification reaction conditions employing as a catalyst an acidic synthetic porous crystalline zeolite having an X-ray diffraction pattern including the lines set forth in Table I, infra. The ether, or mixture of ethers, resulting from the foregoing process can be advantageously employed as blending components for gasoline or as cosolvents for methanol to be incorporated into gasoline, among other applications. The present invention is applicable to the reaction of individual olefins and mixtures of olefins, preferably within the C, ,Q range, with individual alcohols and mixtures of alcohols, preferably those possessing up to 8 carbon atoms and more preferably those possessing from 1 to 4 carbon atoms. Suitable olefins include propylene, butenes, pentenes, hexenes, heptenes and mixtures of these and other olefins such as gas plant off-gas containing ethylene and propylene, naphtha cracker off-gas containing light olefins, fluidized catalytic cracked (FCC) light gasoline containing pentenes, hexenes and heptenes and refinery FCC propane/propylene streams. For example, the following composition is typical for an FCC light olefin stream which can be converted to ethers in accordance with this invention: Ethane Ethylene Propane Propylene Isobutane n-Butane Butenes Pentanes Tertiary olefins are preferred as feedstocks herein with isobutene and/or a tertiary pentene being especially preferred. Suitable alcohols include lower alkanols such as methanol, ethanol, n-propanol, isopropanol and n-butanol and substituted lower alkanols, e.g., methoxy-ethanol. Also contemplated are individual alcohols and mixtures of alcohols which are obtained from the catalytic hydration of olefins in accordance with known and conventional processes. Of the alcohols which are suitable for use herein, the primary and secondary alcohols are preferred with ethanol and methanol being especially preferred. The acidic synthetic porous crystalline zeolite employed as the catalyst of the invention has, in its calcined form, an X-ray diffraction pattern including the lines listed in Table I below: TABLE I Interplanar d-Spacing (A) Relative Intensity, I/Io x 100 M-VS M-S M-VS M-VS W-M -S M-VS VS more specifically the lines listed in Table II below: TABLE II and yet more specifically the lines listed in Table III below: I/Io x 100 cont. Most specifically, the calcined zeolite has an X-ray diffraction pattern including the lines in Table IV below: TABLE IV Interplanar d-Spacing (A) Relative Intensity, I/Io x 100 W-M W M-VS M-S M-VS W-M M-VS W-M W-M W W W-M W W-S W-S M-VS W-M These values were determined by standard techniques. The radiation was the K-alpha doublet of copper and a diffractometer equipped with a scintillation counter and an associated computer was used. The peak heights, I, and the positions as a function of 2 theta, where theta is the Bragg angle, were determined using algorithms on the computer associated with the diffractometer. From these, the relative intensities, 100 I/I 0 , where I 0 is the intensity of the strongest line or peak, and d (obs.) the interplanar spacing in Angstroms Units (A), corresponding to the recorded lines, were determined. In Tables I-IV, the relative intensities are given in terms of the symbols W=weak, M=medium, S=strong and VS=very strong. In terms of intensities, these may be generally designated as follows: W = 0 - 20 M •= 20 - 40 S = 40 - 60 VS = 60 - 100 It should be understood that these X-ray diffraction patterns are characteristic of all species of the present crystalline composition. The sodium form as well as other cationic forms reveal substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the Y to X, e.g., silicon to aluminum, mole ratio of the particular sample, as well as its degree of thermal treatment. I e zeolite employed as the catalyst in the etherification process of this invention has a composition involving the molar relationship: X 2 0 3 :(n)Y0 2 , wherein X is a trivalent element, such as aluminum, boron, iron and/or gallium, preferably aluminum, Y is a tetravalent element such as silicon and/or germanium, preferably silicon, and n is at least 10, usually from 10 to 150, more usually from 10 to 60, and even more usually from 20 to 40. In the as-synthesized form, the zeolite has a formula, on an anhydrous basis and in terms of moles of oxides per n moles of Y0 2 , as follows: (0.005-0.l)Na 2 0:(1-4)R:X 2 0-:nY0 2 wherein R is an organic component. The Na and R components are associated with the zeolite as a result of their presence during crystallization, and are easily removed by post-crystallization methods hereinafter more particularly described. The zeolite employed herein is thermally stable and exhibits high surface area (greater than 400 m /gm as measured by the BET [Bruenauer, Emmet and Teller] test) and unusually large sorption capacity when compared to similar crystal structures. In particular, the zeolite exhibits equilibrium adsorption values greater than 4.5 wt.% for cyclohexane vapor and greater than 10 wt.. for n-hexane vapor. As is evident from the above formula, the zeolite is synthesized nearly free of Na cations. It can, therefore, be used as an etherification catalyst with acid activity without an exchange step. To the extent desired, however, the original sodium cations of the as-synthesized material can be replaced in accordance with techniques well known in the art, at least in part, by ion exchange with other cations. Preferred replacing cations include metal ions, hydrogen ions, hydrogen precursor, e.g., ammonium, ions and mixtures thereof. Prior to its use as etherification catalyst, the zeolite should be subjected to thermal treatment to remove part or all of any organic constituent present therein. The zeolite etherification catalyst herein can also be used in intimate combination with another component having etherification catalytic activity, e.g., any of the known catalysts referred to above. Prior to its use in the etherification process of this invention, the zeolite should be dehydrated, at least partially. This can be done by heating the crystals to a temperature in the range of from 200°C to 595°C in an inert atmosphere, such as air, nitrogen, etc. and at atmospheric, subatmospheric or superatmospheric pressures for between 30 minutes to 48 hours. Dehydration can also be performed at room temperature merely by placing the crystalline material in a vacuum, but a longer time is required to obtain a sufficient amount of dehydration. The zeolite employed in the present process can be prepared from a reaction mixture containing sources of alkali or alkaline earth metal (M), e.g., sodium or potassium, cation, an oxide of trivalent element X, e.g, aluminum, an oxide of tetravalent element Y, e.g., silicon, an organic (R) directing agent in the form of hexamethyleneimine, and water, said reaction mixture having a composition, in terms of mole ratios of oxides, within the following ranges: Reactants Useful Preferred In a preferred synthesis method, the Y0 2 reactant contains a substantial amount of solid Y0-, e.g., at least about 30 wt.% solid Y0 2 . Where Y0 2 is silica, the use of a silica source containing at least 50 wt.% solid silica, e.g., Ultrasil (a precipitated, spray dried silica containing 90 wt.% silica) or HiSil (a precipitated hydrated Si0 2 containing 87 wt.% silica, 6 wt.% free H 2 0 and 4.5 wt.% bound H 2 0 of hydration and having a particle size of 0.02 micron) favors crystal formation from the above mixture. If another source of oxide of silicon, e.g., Q-Brand (a sodium silicate comprised of about 28.8 wt.% of Si0 2 , 8.9 wt.% Na 2 0 and 62.5 wt.% H 2 0) is used, crystallization may yield little of the required zeolite and impurity phases of other crystal structures, e.g., ZSM-12, may be produced. Preferably, therefore, the Y0 2 , e.g., silica, source contains at least about 30 wt.% solid Y0 2 , e.g., silica, and more preferably at least about 40 wt.% solid Y0 2 , e.g., silica. Crystallization can be carried out at either static or stirred conditions in a suitable reactor vessel such as, e.g., polypropylene jars or teflon-lined or stainless steel autoclaves. Crystallization is generally conducted at a temperature of 80°C to 225°C for 25 hours to 60 days. Thereafter, the crystals are separated from the liquid and recovered. Crystallization is facilitated by the presence of at least 0.01 percent, preferably 0.10 percent and still more preferably 1 percent, seed crystals (based on total weight) of the crystalline product. Prior to use in the process of the invention, the resultant zeolite may be combined with another material which is resistant to the temperatures and other conditions employed in the etherification process of this invention. Such materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and/or metal oxides such as alumina. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Use of a material in conjunction with the present zeolite, i.e., combined therewith or present during its synthesis, which itself is catalytically active may change the conversion and/or selectivity of the catalyst. Inactive materials suitably serve as diluents to control the amount of conversion so that ether products can be obtained economically and orderly without employing other means for controlling the rate of reaction. These materials may be incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the catalyst under commercial etherification operating conditions. Said materials, i.e., clays, oxides, etc., function as binders for the catalyst. It is desirable to provide a catalyst having good crush strength because in commercial.use, it is desirable to prevent the catalyst from breaking down into powder-like materials. These clay binders have been employed normally only for the purpose of improving the crush strength of the catalyst. Naturally occurring clays which can be composited with the present zeolite include the montmorillonite and kaolin family, which families include the subbentonites, and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification. Binders useful for compositing with the zeolite also include inorganic oxides, notably alumina. In addition to the foregoing materials, the present zeolite can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia silica-alumina- magnesia and silica-magnesia-zirconia. It may also be advantageous to provide at leat a part of the foregoing matrix materials in colloidal form so as to facilitate extrusion of the bound catalyst component(s). The relative proportions of zeolite and inorganic oxide . matrix vary widely, with the crystal content ranging from 1 to 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads, in the range of 2 to 80 weight percent of the composite. The stability of the etherification catalyst of the invention may be increased by steaming which is conveniently effected by contacting the zeolite with, e.g. , 5 -100%, steam at a temperature of at least 300°C (preferably, 300-650°C) for at least one hour (preferably, 1-200 hours) at a pressure of 101-2,500 kPa. In a more particular embodiment, the catalyst can be made to undergo steaming with 75 -100% steam at 315 -500°C and atmospheric pressure for 2-25 hours. The operating conditions of the etherification process herein are not especially critical and can include a temperature of 20 to 200° C, preferably from 50 to 160°C and most preferably from 60 to 120°C, a total system pressure of from 100 to 20260 kPa (1 to 200 atmospheres) , preferably 300 to 8100 kPa (3 to 80 atmospheres) and most preferably 1000 to 1520 kPa (10 to 15 atmospheres) and an alcohol to olefin mole ratio of 0.1 to 5, preferably from 0.2 to 2 and most preferably from 0.5 to 1.2. The etherification process of this invention can be carried out under liquid phase , vapor phase or mixed vapor- liquid phase conditions in batch or continuous manner using a stirred tank reactor or fixed bed flow reactor, e.g. , trickle-bed, liquid- up- flow, liquid-down-flow, counter-current and co-current flow. Reaction times of 20 minutes to 20 hours when operating in batch and an WHSV (gram-olefin per hour gram zeolite) of 0.01 to 200, preferably 0.5 to 50 and most preferably 1 to 30, when operating continuously are suitable. It is generally preferably to recover any unreacted olefin and/or alcohol and recycle same to the reactor. The etherification process of this invention will now be more particularly described with reference to the following Examples and the accompanying drawings, in which Figures 1-5 are X-ray diffraction patterns of the calcined crystalline material products of Examples 1, 3, 4, 5, and 7, respectively. In the Examples whenever sorption data are set forth for comparison of sorptive capacities for water, cyclohexane and/or n-hexane, they were Equilibrium Adsorption values determined as follows: A weighed sample of the calcined adsorbent was contacted with the desired pure adsorbate vapor in an adsorption chamber, evacuated to less than 1 mm Hg and contacted with 1.6 kPa (12 Torr) of water vapor or 5.5 kPa (40 Torr) of n-hexane or 5.5 kPa (40 Torr) of cyclohexane vapor, pressures less than the vapor-liquid equilibrium pressure of the respective adsorbate at 90 C. The pressure was kept constant (within about _+ 0.5 mm Hg) by addition of adsorbate vapor controlled by a manostat during the adsorption period, which did not exceed about 8 hours. As adsorbate was adsorbed by the crystalline zeolite, the decrease in pressure caused the manostat to open a valve which admitted more adsorbate vapor to the chamber to restore the above control pressures. Sorption was complete when the pressure change was not sufficient to activate the manostat. The increase in weight was calculated as the adsorption capacity of the sample in g/100 g of calcined adsorbant. The zeolite employed herein always exhibits Equilibrium Adsorption values greater than 4.5 wt.%, usually greater than 7 wt.% for cyclohexane vapor, greater than 10 wt.% for n-hexane vapor, and normally greater than 10 wt.% for water vapor. When Alpha Value is examined, it is noted that the Alpha Value is an approximate indication of the catalytic cracking activity of the catalyst compared to a standard catalyst and it gives the relative rate constant (rate of normal hexane conversion per volume of catalyst per unit time). It is based on the activity of a highly active silica-alumina cracking catalyst taken as an Alpha of 1 (Rate Constant = 0.016 sec ). The Alpha Test which is used herein is described in J. Catalysis, 61, pp. 390-396 (1980). It is noted that intrinsic rate constants for many acid-catalyzed reactions are proportional to the Alpha Value for a particular crystalline silicate catalyst, i.e., the rates for toluene disproportionation, xylene isomerization, alkene conversion and methanol conversion (see "The Active Side of Acidic Aluminosilicate Catalysts," Nature, Vol. 509, No. 5969, pp. 589-591, 14 June 1984). EXA>PLE 1 1 part of sodium aluminate (45.5% Al-O.., 52.2% Na 2 0, 25.6% H 2 0) was dissolved in a solution containing 1 part of 50% NaOH solution and 103.15 parts H-0. To this was added 4.50 parts hexamethyleneimine. The resulting solution was added to 8.55 parts of Ultrasil, a precipitated, spray-dried silica (about 90% Si0 2 ). The reaction mixture had the following composition, in mole ratios: where R is hexamethyleneimine. The mixture was crystallized in a stainless steel reactor, with stirring, at 150°C for 7 days. The crystalline product was filtered, washed with water and dried at 120°C. After a 20 hour calcination at 538°C, the X-ray diffraction pattern contained the major lines listed in Table V. Figure 1 shows the X-ray diffraction pattern of the calcined product. The sorption capacities of the calcined material were measured to be: H 2 0 15.2 wt.% Cyclohexane 14.6 wt.% n-Hexane 16.7 wt.% The surface area of the calcined crystalline material was measured to be 494 m 2 /g. The chemical composition of the uncalcined material was determined to be as follows: A portion of the calcined crystalline product of Example 1 was tested in the Alpha Test and was found to have an Alpha Value of 224. EXAMPLES 5-5 Three separate synthesis reaction mixtures were prepared with compositions indicated in Table VI. The mixtures were prepared with sodium aluminate, sodium hydroxide, Ultrasil, hexamethyleneimine (R) and water. The mixtures were maintained at 150°C, 143°C and 150°C, respectively, for 7, 8 and 6 days respectively in stainless steel autoclaves at autogenous pressure. Solids were separated from any unreacted components by filtration and then water washed, followed by drying at 120°C. The product crystals were subjected to X-ray diffraction, sorption, surface area and chemical analyses. The results of the sorption, surface area and chemical analyses are also presented in Table VI and the X-ray diffraction patterns are presented in Figures 2, 3 and 4, respectively. The sorption and surface area measurements were of the calcined product. TABLE VI EXAMPLE 6 Quantities of the calcined (538°C for 5 hours) crystalline silicate products of Examples 5, 4 and 5 were tested in the Alpha Test and found to have Alpha Values of 227, 180 and 187, respectively. EXAMPLE 7 To demonstrate a further preparation of the present zeolite, 4.49 parts of hexamethyleneimine was added to a solution containing 1 part of sodium aluminate, 1 part of 50% NaOH solution and 44.19 parts of H.O. To the combined solution were added 8.54 parts of Ultrasil silica. The mixture was crystallized with agitation at 145°C for 59 hours and the resultant product was water washed and dried at 120°C. The X-ray diffraction pattern of the dried product crystals is presented in Figure 5 and demonstrates the product to be the crystalline material of this invention. Product chemical composition, surface area and adsorption analyses results were as set forth in Table VII: TABLE VII Product Composition (uncalcined) C 12.1 wt.% N 1.98 wt.% Na 640 ppm EXAMPLE 8 25g grams of solid crystal product from Example 7 were calcined in a flowing nitrogen atmospheres at 558°C for 5 hours, followed by purging with 5% oxygen gas (balance N 2 ) for another 16 hours at 538°C. Individual 5g samples of the calcined material were ion-exchanged with 100 ml of 0.1N TEABr, TPABr and LaCl- solution separately. Each exchange was carried out at ambient temperature for 24 hours and repeated three times. The exchanged samples were collected by filtration, water-washed to be halide-free and dried. The compositions of the exchanged samples are tabulated below demonstrating the exchange capacity of the present crystalline silicate for different ions. The La-exchanged sample from Example 8 was sized to 14 to 25 mesh and then calcined in air at 558°C for 5 hours. The calcined material had an Alpha Value of 175. EXAMPLE 10 The calcined sample La-exchanged material from Example 9 was severely steamed at 649°C in 100% steam for 2 hours. The steamed sample had an Alpha Value of 22, demonstrating that the zeolite had very good stability under severe hydrothermal treatment. EXAMPLE 11 This example illustrates the preparation of the present zeolite where X in the general formula, supra, is boron. Boric acid, 2.59 parts, was added to a solution containing 1 part of 45% KOH solution and 42.96 parts H.O. To this was added 8.56 parts of Ultrasil silica, and the mixture was thoroughly homogenized. A 3.88 parts quantity of hexamethyleneimine was added to the mixture. The reaction mixture had the following composition in mole ratios: Si0 2 /B 2 0- = 6.1 0H " /Si0 2 = 0.06 H 2 0/Si0 2 = 19.0 K/SiO- = 0.06 R/Si0 2 = 0.30 where R is hexamethyleneimine. The mixture was crystallized in a stainless steel reactor, with agitation, at 150°C for 8 days. The crystalline product was filtered, washed with water and dried at 120°C. A portion of the product was calcined for 6 hours at 540°C and found to have the following sorption capacities: H 2 0 (12 Torr) 11.7 wt.% Cyclohexane (40 Torr) 7.5 wt.% n-Hexane (40 Torr) 11.4 wt.% The surface area of the calcined crystalline material was measured (BET) to be 405m 2 /g. The chemical composition of the uncalcined material was determined to be as follows: N 1.94 wt.% Na 175 ppm K 0.60 wt.% Boron 1.04 wt.% A1 2 0- 920 ppm Si0 2 75.9 wt.% Ash 74.11 wt.% SiO-/Al 2 0-, molar ratio = 1406 Si0 2 /(A1+B) 2 0 3 , molar ratio = 25.8 EXAMPLE 12 A portion of the calcined crystalline product of Example 11 was treated with NH.C1 and again calcined. The final crystalline product was tested in the Alpha Test and found to have an Alpha Value of 1. EXAMPLE 13 This example illustrates another preparation of the zeolite in which X of the general formula, supra, is boron. Boric acid, 2.23 parts, was added to a solution of 1 part of 50% NaOH solution and 73.89 parts H_0. To this solution was added 15.29 parts of HiSil silica followed by 6.69 parts of hexamethyleneimine. The reaction mixture had the following composition in mole ratios: Si0 2 /B 2 0 3 = 12.3 0H " /Si0 2 = 0.056 H~0/Si0 2 = 18.6 K/Si0 2 = 0.056 R/Si0 2 = 0.30 where R is hexamethyleneimine. The mixture was crystallized in a stainless steel reactor, with agitation, at 300°C for 9 days. The crystalline product was filtered, washed with water and dried at 120°C. The sorption capacities of the calcined material (6 hours at 540°C) were measured: H 2 0 14.4 wt.% Cyclohexane 4.6 wt.% n-Hexane 14.0 wt.% The surface area of the calcined crystalline material was measured to be 438m /g. The chemical composition of the uncalcined material was determined to be as follows: 28. A portion of the calcined crystalline product of Example 13 was tested in the Alpha Test and found to have an Alpha Value of 5. EXAMPLES 15-45 These examples compare the etherification catalyst performance for three zeolites: ZSM-5 of about 70:1 Si/Al-0 3 mole ratio (Examples 15 to 25), USY of about 6:1 Si/Al-,0-, mole ratio (Examples 26 to 55) and the zeolite of the invention of about 26:1 Si/Al 2 0 3 mole ratio (54 to 45). The zeolite of the invention was prepared by adding 4.49 parts of hexamethyleneimine was added to a mixture containing 1.00 part sodium aluminate, 1.00 part 50% NaOH, 8.54 parts Ultrasil VN5 and 44.19 parts deionized H-0. The reaction mixture was heated to 145°C (290°F) and stirred in an autoclave at that temperature for crystallization. After full crystallinity was achieved, the majority of the hexamethyleneimine was removed from the autoclave by controlled distillation and the zeolite crystals separated from the remaining liquid by filtration, washed with deionized H 2 0 and dried. A portion of the zeolite crystals was combined with 1 2 0 3 to form a mixture of 65 parts, by weight, zeolite and 55 parts Al-0 3 . Water was added to this mixture to allow the resulting catalyst to be formed into extrudates. The catalyst was activated by calcining in nitrogen at 540°C (1000°F) for six hours, followed by aqueous ammonium nitrate exchange and calcining in air at 540°C (1000°F) for six hours. In all examples, methanol and either isobutene or isoaraylene (isopentene) were introduced at various space velocities ranging from 2 to 200 into an up-flow ixed bed reactor charged with one of the foregoing zeolite catalysts diluted to about 10% (vol.) in sand to constant volume. The reaction conditions and results for each examples are set forth in Tables VIII, IX and X as follows: sjαripαy ID poseg UDisjaΛUoj \ _. * _ 06'T \L'L __'SI (K'W Lϊ ' i 16 ' K 90 ' £ l * Z7l ZI " 9Z KTS ("ΪPI°) Λ9M IZ7 K)7 _8'l 117 GG' l 89 * 1 Z0 98' t £07 S6 * l £07 "^lO/llH^ opea _[cw (HSl)SOZ (t-TSI)SOZ (HSI)SOZ (IZSI)90Z (S£SI)80Z (HSt)SOZ (8ZSt) 0Z (HSI)SOZ (HSΪ)SOZ (HSOSOZ (frlSI)SOZ (*tf * 1) tsd 'amssay OOt 66 OOt 001 Kit 001 tOt 86 001 ZOf 66 ' o , , d-BL C6T IM 891 S9I £91 Z9I SK £fr t * Z 11 81 mS-UlS «> SJ» — suaHBttost — » ■< ■ ■ sυs xpst •^ = -- — » suoμtpucr) unsjaiuicr) SZ t_ £Z ZZ IZ OZ 6r 8f L\ 91 SI θittuexg sXiB -o tpμeDijμ g ipg s-lEZ IIIΛ -navj. sj irpαy ID poseg uoisjaΛuor) $ Z6'96 PL'IS Z9'S6 OZ OZ 86'66Z Z6'9l- 9£70I 96'WZ (UTjap) Λ3M 107 W7 66 * 1 I6't 007 WI Z07 Z07 "JFPIOlrø oμey (HSl)SOZ (t-ISt)SOZ (frlSDSOZ (t-ISl)SOZ (HSt)SOZ (6l * Sl)0tZ (frISDSOZ (MSl)SOZ (W) isd 'amssay tot lOt ΪOt lOt ZOI 101 lOf OOt a, • • ΛBL £Z IZ £ £ I__ ZZ S £_ < - ■ auajifcxfast ___Qiϊ|osr >■ IsXprna tppEHjμsφg sn XI 3TSVL Pressure, PS1 (kPa) 200(1480) 200(1480) 200(1480) 200(1480) 200(1480) 240(1756) 210(1549) 210(1549) 210(1549) Mole Ratio MeOH/Olefin 1.99 2.53 2.61 1.96 1.98 2.04 1.89 2.01 1.96 WHSV (olefin) 16.56 28.87 4.19 34.20 8.29 4.13 8.80 21.01 5.40 1 ON ∞ OeN The activities of the three etherification catalysts compared in Examples 15-43 were quantified using the following rate law: In (1 - ) = eq • " • eq WHSV where k is the pseudo first order rate constant, X is the olefin conversion, and X eq , the value of conversion at equilibrium, has experimental values of 95% for isobutene and 51% for isoaraylene for the foregoing etherification reaction conditions. Comparison of the kinetics of etherification for the three zeolite catalysts are set forth in Table XI as follows : TABLE XI In Table XI, Performance Ratio (PR) quantifies the rate at which isoamylene is consumed by methanol relative to the rate for isobutene. In a mixed feed process, it is generally desirable that this ratio be at least 10 and preferably greater than 15. A ratio of 100 indicates that olefins of both low and high carbon numbers will tend to be consumed at comparable rates. Of the three zeolite catalysts, USY has the better TAME/MTBE PR. However, the rate constants for USY show that this catalyst has a very low activity. Both ZSM-5 and the catalyst of the invention have acceptably higher activity. However, in contrast, the catalyst of the invention has the superior combination of good activity with desirable selectivity as shown by its PR. ■ 27 — EXAMPLES 44-46 These examples illustrate the preparation of ethyl tertiary-butyl ether (ETBE) which is useful, among other applications, as a high octane blending stock for gasoline, employing as catalyst, 65 wt.% zeolite in 55 wt.% alumina (binder) in accordance with this invention. The conditions under which ethanol was reacted with isobutene in each example and the results obtained are set forth in Table XII as follows: TABLE XII

Claims: CLAIMS: 1. A process for manufacturing an ether or mixture of ethers which comprises reacting at least one olefin with at least one alcohol under etherification reaction conditions employing as a catalyst an acidic synthetic porous crystalline zeolite having an X-ray diffraction pattern with the lines as set forth in Table I of the specification. 2. The process of Claim 1 wherein the zeolite has an X-ray diffraction pattern with the lines set forth in Table II of the specification. 5. The process of Claim 1 wherein the zeolite has an X-ray diffraction pattern with the lines set forth in Table III of the specification. 4. The process of Claim 1 wherein the zeolite has an X-ray diffraction pattern with the lines set forth in Table IV of the specification. 5. The process of any one of Claims 1 to 4 wherein the zeolite has equilibrium adsorption capacities greater than 4.5 wt.% for cyclohexanes vapor and greater than 10 wt.% for n-hexane vapor. 6. The process of any one of Claims 1 to 4 wherein the zeolite has a composition comprising the molar relationship X 2 0 3 :(n)YO 2 , wherein n is at least 10, X is a trivalent element and Y is a tetravalent element. 7. The process of Claim 6 wherein X comprises aluminum and Y comprises silicon. 8. The process of any one of Claims 1 to 4 wherein the olefin has 5 to 10 carbon atoms. 9. The process of Claim 8 wherein the olefin is an isobutene or isopentene. 10. The process of Claim 8 wherein the alcohol possesses up to 8 carbon atoms. 11. The process of Claim 9 wherein the alcohol is methanol, ethanol, n-propanol, isopropanol or a butanol or a mixture thereof. 12. The process of any one of Claim 1 to 4 wherein the etherification reaction conditions include a temperature of 20 to 200°C, a total system pressure of 100 to 20260 kPa (1 to 200 atmospheres) and an olefin to alcohol mole ratio of 0.1 to 5.

Inventors: BELL WELDON KAY, HAAG WERNER OTTO, MARLER DAVID OWEN, BELL, WELDON, KAY, HAAG, WERNER, OTTO, MARLER, DAVID, OWEN
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1990
Main classification: C07C41
IPC codes: B01J29, C07B61, C07C41, C07C43