ZEOLITE SSZ-42

Abstract: The present invention relates to new crystalline zeolite SSZ-42 prepared by processes for preparing crystalline molecular sieves, particularly large pore zeolites, using an organic templating agent selected from the group consisting of N-benzyl-1,4-diazabicyclo[2.2.2]octane cations and N-benzyl-1-azabicyclo[2.2.2]octane cations.

Description: ZEOLITE SSZ-42 BACKGROUND OF THE INVENTION Field of the Invention The present invention relates to new crystalline zeolite SSZ-42 prepared using an N-benzyl-1,4- diazabicyclo[2.2.2]octane cation or N-benzyl-1- azabicyclo[2.2.2]octane cation templating agent, and hydrocarbon conversion processes using SSZ-42 as a catalyst. State of the Art in conventional usage the term "molecular sieve" refers to a material having a fixed, open-network structure, usually crystalline, that may be used to separate hydrocarbons or other mixtures by selective occlusion of one or more of the constituents, or may be used as a catalyst in a catalytic conversion process. The term "zeolite" refers to a molecular sieve containing a silicate lattice, usually in association with some aluminum, boron, gallium, iron, and/or titanium. In the following discussion and throughout this disclosure, the terms molecular sieve and zeolite will be used more or less interchangeably. One skilled in the art will recognize that the teachings relating to zeolites are also applicable to the more general class of materials called molecular sieves. Natural and synthetic crystalline molecular sieves are useful as catalysts and adsorbents. Each crystalline molecular sieve is distinguished by a crystal structure with an ordered pore structure, and is characterized by a unique X-ray diffraction pattern. Thus, the crystal structure 01 defines cavities and pores which are characteristic of the 02 different species. The adsorptive and catalytic properties 03 of each crystalline molecular sieve are determined in part 04 by the dimensions of its pores and cavities. Accordingly, 05 the utility of a particular molecular sieve in a particular 06 application depends at least partly on its crystal 07 structure. 08 09 Because of their unique sieving characteristics, as well as 10 their catalytic properties, crystalline molecular sieves are 11 especially useful in applications such as hydrocarbon 12 conversion, gas drying and separation. Although many 13 different crystalline molecular sieves have been disclosed, 14 there is a continuing need for new zeolites with desirable 15 properties for gas separation and drying, hydrocarbon and 16 chemical conversions, and other applications. 17 18 Crystalline aluminosilicates are usually prepared from 19 aqueous reaction mixtures containing alkali or alkaline 20 earth metal oxides, silica, and alumina. Crystalline 21 borosilicates are usually prepared under similar reaction 22 conditions except that boron is used in place of aluminum. 23 By varying the synthesis conditions and the composition of 24 the reaction mixture, different zeolites can often be 25 formed. 26 27 Organic templating agents are believed to play an important 28 role in the process of molecular sieve crystallization. 29 Organic amines and quaternary ammonium cations were first 30 used in the synthesis of zeolites in the early 1960s as 31 reported by R. M. Barrer and P. J. Denny in J. Chem. Soc. 32 1961 at pages 971-982. This approach led to a significant 33 increase in the number of new zeolitic structures discovered 3.4 as well as an expansion in the boundaries of composition of the resultant crystalline products. Previously, products with low silica to alumina ratios (Si0 2 /Al 2 0 3 ≤ 10) had been obtained, but upon using the organocations as components in the starting gels, zeolites with increasingly high Si0 2 /Al 2 0 3 were realized. Some of these materials are summarized by R. H. Barrer 1982, Hydrothermal Chemistry of Zeolites , New York: Academic Press, Inc. Unfortunately, the relationship between structure of the organocation and the resultant zeolite is far from predictable, as evidenced by the multitude of products which can be obtained using a single quaternary ammonium salt as reported by S. I. Zones et al., 1989, Zeolites: Facts, figures, .Future, ed. P. A. Jacobs and R. A. van Santen, pp. 299-309, Amsterdam: Elsevier Science Publishers, or the multitude of organocations which can produce a single zeolitic product as reported by R. M. Barrer, 1989, Zeolite Synthesis, ACS Symposium 398, ed. M. L. Occelli and H. E. Robson, pp. 11-27, American Chemical Society. Thus, it is known that organocations exert influence on the zeolite crystallization process in many unpredictable ways. Aside from acting in a templating role, the organic cation's presence also greatly affects the characteristics of the gel. These effects can range from modifying the gel pH to altering the interactions of the various components via changes in hydration (and thus solubilities of reagents) and other physical properties of the gel. Accordingly, investigators have now begun to consider how the presence of a particular quaternary ammonium salt influences many of these gel characteristics in order to determine more rigorously how such salts exert their templating effects. u. S. Patent No. 5,194,235, issued March 6, 1993 to Zones, discloses the use of a templating agent known as DABCO-C a -diquat to prepare the zeolite SSZ-16. This templating agent has the following formula: wherein n is 3, 4 or 5. In summary, a variety of templates have been used to synthesize a variety of molecular sieves, including zeolites of the silicate, aluminosilicate, and borosilicate families. However, the specific zeolite which may be obtained by using a given template is at present unpredictable. In fact, the likelihood of any given organocation serving as an effective template useful in the preparation of a molecular sieve is conjectural at best. In particular, organocation templating agents have been used to prepare many different combinations of oxides with molecular sieve properties, with silicates, aluminosilicates, aluminophosphates, borosilicates and silicoaluminophosphates being well known examples. SUMMARY OF THE INVENTION in accordance with the present invention there is provided a zeolite having a mole ratio of an oxide selected from silicon oxide, germanium oxide and mixtures thereof to an oxide selected from aluminum oxide, gallium oxide, iron oxide, titanium oxide, boron oxide and mixtures thereof 1 greater than about 10 and having the X-ray diffraction lines 2 of Table I. 3 4 The present invention also provides a zeolite having an 5 average pore size diameter greater than about 6 Angstroms 6 and having the X-ray diffraction lines of Table II. 7 8 in accordance with the present invention there is further 9 provided a zeolite having a composition, as-synthesized and 0 in the anhydrous state, in terms of mole ratios as follows: 1 2 Y0 2 / 2 0 3 Greater than or equal to 15 3 Y0 2 /M 2 0 Greater than or equal to 45 Y0 2 /Q 10-40 5 * wherein Q is comprised of cations selected from the group 7 consisting of N-benzyl-l,4-diazabicyclo[2.2.2]octane cations 8 and N-benzyl-l-azabicyclo[2.2.2]octane cations, M is an ' alkali metal cation or alkaline earth metal cation, W is a 0 trivalent atom selected from the group consisting of boron, 1 aluminum, gallium, iron, titanium, and mixtures thereof 2 wherein at least 50% of is boron, and Y is selected from 3 the group consisting of silicon, germanium, and mixtures 4 thereof and having the X-ray diffraction lines of Table I. 5 6 In accordance with this invention, there is also provided a 7 zeolite prepared by thermally treating (calcining) a zeolite 8 having a mole ratio of an oxide selected from silicon oxide, 9 germanium oxide and mixtures thereof to an oxide selected 0 from aluminum oxide, gallium oxide, iron oxide, titanium 1 oxide, boron oxide and mixtures thereof greater than about 2 ιo and having the X-ray diffraction lines of Table I at a 3 temperature of from about 200°C (392°F) to about 800 β C 4 (1472 β F) , the thus-treated zeolite having the X-ray diffraction lines of Table II. The present invention also includes the hydrogen form of this thus-prepared zeolite, which hydrogen form is prepared by ion exchanging with an acid or with a solution of an ammonium salt followed by a second thermal treatment. in accordance with the present invention there is also provided a catalyst comprising the aforesaid hydrogen form of the zeolite of this invention. The present invention additionally provides a process for converting hydrocarbons comprising contacting a hydrocarbonaceous feed at hydrocarbon converting conditions with the catalyst of this invention. Further provided by the present invention is a hydrocracking process comprising contacting a hydrocarbon feedstock under hydrocracking conditions with the catalyst of this invention. This invention also includes a dewaxing process comprising contacting a hydrocarbon feedstock under dewaxing conditions with the catalyst of this invention. Also included in this invention is a process for increasing the octane of a hydrocarbon feedstock to produce a product having an increased aromatics content comprising contacting a hydrocarbonaceous feedstock which comprises normal and slightly branched hydrocarbons having a boiling range above about 40 β C (104*F) and less than about 300 β C (572 β F) , under aromatic conversion conditions with the zeolite of this invention. Also provided in this invention is such a process wherein the zeolite contains a Group VIII metal component. 1 Also provided by the present invention is a catalytic 2 cracking process comprising contacting a hydrocarbon 3 feedstock in a reaction zone under catalytic cracking 4 conditions in the absence of added hydrogen with a catalyst 5 comprising the aforementioned hydrogen form of the zeolite 6 of this invention. 7 8 Also included in this invention is such a catalytic cracking 9 process wherein the catalyst additionally comprises a large 0 pore crystalline cracking component. 1 2 The present invention further provides an isomerizing 3 process for isomerizing C 4 to G-. hydrocarbons, comprising 4 contacting a catalyst, comprising at least one Group VIII 5 metal and the hydrogen form catalyst of this invention, with 6 a feed having normal and slightly branched C 4 to C** 7 hydrocarbons under isomerizing conditions. 8 ' Also provided is such an isomerization process wherein the 0 catalyst has been calcined in a steam/air mixture at an 1 elevated temperature after impregnation of the Group VIII 2 metal, preferably platinum. 3 4 This invention also provides a process for alkylating an 5 aromatic hydrocarbon which comprises contacting under 6 alkylation conditions at least a molar excess of an aromatic 7 hydrocarbon with a C j to C^, olefin under at least partial 8 liquid phase conditions and in the presence of the hydrogen 9 form catalyst of this invention. 0 1 This invention additionally provides a process for 2 transalkylating an aromatic hydrocarbon which comprises 3 contacting under transalkylating conditions an aromatic ^ hydrocarbon with a polyalkyl aromatic hydrocarbon under at least partial liquid phase conditions and in the presence of the hydrogen form catalyst of this invention. Further provided by this invention is a process to convert paraffins to aro atics which comprises contacting paraffins with the hydrogen form catalyst of this invention, said catalyst comprising gallium, zinc, lead or indium or a compound of gallium, zinc, lead or indium. This invention also provides a process for converting lower alcohols and other oxygenated hydrocarbons comprising contacting said lower alcohol or other oxygenated hydrocarbon with the hydrogen form catalyst of this invention under conditions to produce liquid products. This invention also provides a process for isomerizing olefins comprising contacting said olefin with the catalyst of this invention in its hydrogen form under conditions which cause isomerization of the olefin. One example of such a process is the isomerization of n-butene to isobutene. The full scope of the present invention will be apparent to those familiar with molecular sieve synthesis from the following detailed description of the principle features of SSZ-42 and from the examples which accompany the description. BRIEF DESCRIPTION OF THE DRAWING The drawing is a graph showing run hours versus temperature for a reforming reaction using the catalyst of this invention (plot A) , a commercially available catalyst (plots B and B') and a platinum-containing cesium beta zeolite catalyst (plots C and C). DETAILED DESCRIPTION OF THE INVENTION Principle Features The present invention comprises a family of crystalline multidimensional large pore zeolites, SSZ-42. As used herein the term "large pore" means having an average pore size diameter greater than about 6 Angstroms, preferably from about 6.5 Angstroms to about 7.5 Angstroms. SSZ-42 zeolites can be prepared from an aqueous solution comprising sources of an alkali or alkaline earth metal oxide, the templating agent, and sources of the desired trivalent element oxides and tetravalent element oxides. The reaction mixture should have a composition, in terms of mole ratios, within the ranges shown in Table A. wherein Q is comprised of cations selected from the group consisting of N-benzyl-l,4-diazabicyclo[2.2.2]octane cations and N-benzyl-l-azabicyclo[2.2.2]octane cations, M is an alkali metal cation or alkaline earth metal cation, W is selected from the group aluminum, gallium, iron, boron, titanium and mixtures thereof wherein at least 50% of W is boron, and Y is selected from the group consisting of silicon, germanium, and mixtures thereof. SSZ-42 can be made essentially aluminum free, i.e., having a silica to alumina mole ratio of ∞. The term "essentially alumina-free" is used because it is difficult to prepare completely aluminum-free reaction mixtures for synthesizing these materials. Especially when commercial silica sources are used, aluminum is almost always present to a greater or lesser degree. The hydrothermal reaction mixtures from which the essentially alumina-free crystalline siliceous molecular sieves may be prepared can be referred to as being substantially alumina free. By this usage is meant that no aluminum is intentionally added to the reaction mixture, e.g., as an alumina or aluminate reagent, and that to the extent aluminum is present, it occurs only as a contaminant in the reagents. An additional method of increasing the mole ratio of silica to alumina is by using standard acid leaching or chelating treatments. However, essentially aluminum-free SSZ-42 can be synthesized directly using essentially aluminum-free silicon sources as the only tetrahedral metal oxide component. SSZ-42 can also be prepared directly as a borosilicate, or as an alumino(boro)silicate by first preparing SSZ-42 as a borosilicate and then substituting aluminum for at least a portion of the boron by post synthesis treatment of the borosilicate. Lower silica to alumina ratios may also be obtained by using methods which insert aluminum into the crystalline framework. For example, aluminum insertion may occur by thermal treatment of the zeolite in combination with an alumina binder or dissolved source of alumina. Such procedures are described in U.S. Patent No. 4,559,315, issued December 17, 1985 to Chang et al., which is incorporated by reference herein in its entirety. SSZ-42 as-synthesized has a mole ratio of tetravalent element oxides selected from silicon oxide, germanium oxide, and mixtures thereof to trivalent element oxides selected from aluminum oxide, gallium oxide, iron oxide, boron oxide, titanium oxide and mixtures thereof greater than about 10 wherein at least 50% of the trivalent element oxide is boron oxide; and has the X-ray diffraction lines of Table I below. SSZ-42 further has a composition, as-synthesized and in the anhydrous state, in terms of mole ratios indicated in Table B below. TABLE B AS-SYNTHESIZED SSZ-42 Y0 2 /W 2 0 3 Greater than or equal to 15 Y0 2 /M 2 0 Greater than or equal to 45 Y0 2 /Q 10-40 wherein Q, Y, W and M are as defined above, and wherein at least 50% of W is boron. x is believed that SSZ-42 is comprised of a new framework structure or topology which is characterized by its X-ray diffraction pattern. SSZ-42 zeolites, as-synthesized, have crystalline structure whose X-ray powder diffraction pattern exhibit the characteristic lines shown in Table I and is thereby distinguished from other known zeolites. After calcination, the SSZ-42 zeolites have a crystalline structure whose X-ray powder diffraction pattern include the characteristic lines shown in Table II: TABLE II CALCINED SSZ-42 2Theta d/n 100 I/I- 9 8.22 10.75 100 9.76 9.06 13 0 16.42 5.394 3 1 19.22 4.615 7 20.48 4.333 30 20.84 4.259 25 21.48 4.134 7 21.72 4.088 16 23.68 3.754 6 6 24.06 3.696 15 7 24.94 3.568 10 8 25.40 3.504 6 9 26.60 3.348 20 0 29.56 3.019 10 1 2 The variation in the scattering angle (two theta) measurements, due to instrument error and to indifferences 4 between individual samples, is estimated at +/- 0.20 5 degrees. 6 7 Representative peaks from the X-ray diffraction pattern of 8 calcined SSZ-42 are shown in Table II. Calcination can also « result in-changes in the intensities of the peaks as 0 compared to patterns of the "as-synthesized" material, as 1 well as minor shifts in the diffraction pattern. The 2 zeolite produced by exchanging the metal or other cations 3 present in the zeolite with various other cations (such as 4 H + or NH 4 + ) yields essentially the same diffraction pattern, although again, there may be minor shifts in the interplanar spacing and variations in the relative intensities of the peaks. Notwithstanding these minor perturbations, the basic crystal lattice remains unchanged by these treatments. The X-ray powder diffraction patterns were determined by standard techniques. The radiation was the K-alpha/doublet of copper. A scintillation counter spectrometer with a strip-chart pen recorder was used. The peak heights I and the positions, as a function of 20 where θ is the Bragg angle, were read from the relative intensities, I/I 0 where I 0 is the intensity of the strongest line or peak, and d, the interplanar spacing in Angstroms corresponding to the recorded lines, can be calculated. The Preparation of SSZ-42 Zeolites in preparing SSZ-42 zeolites, an N-benzyl-1,4- diazabicyclo[2.2.2]octane cation or N-benzyl-1-aza- bicyclo[2.2.2]octane cation may be used as a crystallization template in a manner known in the molecular sieve art. Thus, in general, SSZ-42 is prepared by contacting an active source of one or more oxides selected from the group consisting of onovalent element oxides, divalent element oxides, trivalent element oxides, and tetravalent element oxides with an organocation templating agent. in practice, SSZ-42 is prepared by a process comprising: (a) preparing an aqueous solution containing sources of the oxides listed in Table A above and at least one N-benzyl-l,4-diazabicyclo[2.2.2]octane cation or N- benzyl-l-azabicyclo[2.2.2]octane cation templating agent having an anionic counterion which is not detrimental to the formation of SSZ-42; (b) maintaining the aqueous solution under conditions sufficient to form crystals of SSZ-42; and (c) recovering the crystals of SSZ-42. The N-benzyl-l,4-diazabicyclo[2.2.2]octane cation and N- benzyl-l-azabicyclo[2.2.2]octane cation templating agents which have been found to produce SSZ-42 have the following general formulas: Λ where R is —H, —OH or —NH 2 . ' Examples of the N-benzyl-l,4-diazabicyclo[2.2.2]octane cation templating agents useful in this invention include, but are not limited to, N-benzyl-1,4- diazabicyclo[2.2.2]octane cation, and examples of the N-benzyl-l-azabicyclo[2.2.2]octane cation templating agents useful in this invention include, but are not limited to, N-benzyl-l-azabicyclo[2.2.2]octane cation and N-benzyl-3- hydroxy-l-azabicyclo[2.2.2]octane cation. SSZ-42 may comprise the crystalline material and the templating agent in combination with metallic and non-metallic oxides bonded in tetrahedral coordination through shared oxygen atoms to form a cross-linked three dimensional crystal structure. The metallic and non-metallic oxides comprise one or a combination of oxides selected from the group consisting of one or more trivalent element(s) , and one or more tetravalent element(s) . The trivalent element is preferably selected from the group consisting of aluminum, boron, gallium, iron, titanium with at least 50% of the trivalent element being boron. Once the as-synthesized SSZ-42 material has been made, some or all of the boron may be replaced with, e.g., aluminum. Thus, in the calcined version of SSZ-42, the trivalent element is preferably aluminum, boron or combinations thereof. The tetravalent element is preferably selected from the group consisting of silicon, germanium, and combinations thereof. More preferably, the tetravalent element is silicon. Typical sources of silicon oxide include silicates, silica hydrogel, silicic acid, fumed silica, colloidal silica, tetra-alkyl orthosilicates, and silica hydroxides. Boron, as well as gallium, germanium, titanium, and iron can be added in forms corresponding to their silicon counterparts, i.e, as borates, boric acid and the like. Typical sources of aluminum oxide for the reaction mixture include aluminates, alumina and aluminum compounds such as AlCl j , A1(S0 4 ) 3 , hydrated Al(OH) 3 gels, kaolin clays, colloidal aluminas, and the like. Alternatively, a zeolite reagent may provide a source of aluminum or boron. In some cases, the source zeolite may provide a source of silica. In that case, the source zeolite in its dealu inated or deboronated form may be used as a source of silica, with additional silicon added using, for example, the conventional sources listed above. Use of a source zeolite reagent as a source of alumina for the present process is described in U.S. Patent No. 4,503,024 01 issued on March 5, 1985 to Bourgogne, et al. entitled 02 "PROCESS FOR THE PREPARATION OF SYNTHETIC ZEOLITES, AND 03 ZEOLITES OBTAINED BY SAID PROCESS", the disclosure of which 4 is incorporated herein by reference. 5 6 Typically, an alkali metal hydroxide and/or an alkaline 7 earth metal hydroxide, such as the hydroxide of sodium, 8 potassium, lithium, cesium, rubidium, calcium, and 9 magnesium, is used in the reaction mixture; however, this 0 component can be omitted so long as the equivalent basicity 1 is maintained. The templating agent may be used to provide 2 hydroxide ion. Thus, it may be beneficial to ion exchange, 3 for example, a hydroxide anion for a halide ion in the 4 templating agent, thereby reducing or eliminating the alkali 5 or alkaline earth metal hydroxide quantity required. The 6 alkali metal cation or alkaline earth cation may be part of 7 the as-synthesized crystalline oxide material, in order to 8 balance valence electron charges therein. 9 0 The reaction mixture is maintained at an elevated 1 temperature until the crystals of the SSZ-42 zeolite are 22 formed. This hydrothermal crystallization is usually 3 conducted under autogenous pressure, at a temperature 24 between 100 β C (212 β F) and 200°C (392 β F), preferably between 25 135* (275 β F) and 180 β C (356 β F) . The crystallization period 26 is typically greater than 1 day and preferably from about 3 27 days to about 7 days. The zeolite can be prepared with or 28 without mild stirring or agitation. 29 30 During the hydrothermal crystallization step, the SSZ-42 31 crystals can be allowed to nucleate spontaneously from the 32 reaction mixture. However, the use of SSZ-42 crystals as 33 seed material can be advantageous in decreasing the time 3.4 necessary for complete crystallization to occur. In 01 addition, seeding can lead to an increased purity of the 02 product obtained by promoting the nucleation and/or 03 formation of SSZ-42 over any undesired phases. When used as 04 seeds, SSZ-42 crystals are added in an amount between 0.1 05 and 10% of the weight of silica used in the reaction 06. mixture. 07 08 Once the zeolite crystals have formed, the solid product is 09 separated from the reaction mixture by standard mechanical 10 separation techniques such as filtration. The crystals are 11 water-washed and then dried, e.g., at 90 β C (194°F) to 150°C 12 (302°F) for from 8 to 24 hours, to obtain the 13 as-synthesized, SSZ-42 zeolite crystals. The drying step 14 can be performed at atmospheric pressure or under vacuum. 15 16 Crystalline SSZ-42 can be used as-synthesized or can be 17 thermally treated (calcined) . Usually, it is desirable to 18 remove the alkali or alkaline earth metal cation by ion 19 exchange and replace it with hydrogen, ammonium, or any 20 desired metal ion. The zeolite can be leached with 21 chelating agents, e.g., EDTA or dilute acid solutions, to 22 increase the silica to alumina mole ratio. The zeolite can 23 also be steamed; steaming helps stabilize the crystalline 24 lattice to attack from acids. The zeolite can be used in 25 intimate combination with hydrogenating components, such as 26 tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, 27 chromium, manganese, or a noble metal, such as palladium or 28 platinum, for those applications in which a 29 hydrogenation-dehydrogenation function is desired. 30 31 Metals may also be introduced into the zeolite by replacing 32 some of the cations in the zeolite with metal cations via 33 ion exchange techniques. Typical replacing cations can 34 include metal cations, e.g., rare earth, Group IIA and Group VIII metals, as well as their mixtures. Of the replacing metallic cations, cations of metals such as rare earth, Mn, Ca, Mg, Zn, Cd, Pt, Pd, Ni, Co, Ti, Al, Sn, and Fe are particularly preferred. The hydrogen, ammonium, and metal components can be ion-exchanged into the SSZ-42. The zeolite can also be impregnated with the metals, or the metals can be physically and intimately admixed with the zeolite using standard methods known to the art. Typical ion-exchange techniques involve contacting the synthetic zeolite with a solution containing a salt of the desired replacing cation or cations. Although a wide variety of salts can be employed, chlorides and other halides, acetates, nitrates, and sulfates are particularly preferred. The zeolite is usually calcined prior to the ion-exchange procedure to remove the organic matter present in the channels and on the surface, since this results in a more effective ion exchange. Representative ion exchange techniques are disclosed in a wide variety of patents including U.S. Patent Nos. 3,140,249 issued on July 7, 1964 to Plank, et al.; 3,140,251 issued on July 7, 1964 to Plank, et al.; and 3,140,253 issued on July 7, 1964 to Plank, et al., each of which is incorporated by reference herein. Following contact with the salt solution of the desired replacing cation, the zeolite is typically washed with water and dried at temperatures ranging from 65°C (149°F) to about 200 β C (392 β F). After washing, the zeolite can be calcined in air or inert gas at temperatures ranging from about 200°C (392 β F) to about 800°C (1472 β F) for periods of time ranging from 1 to 48 hours, or more, to produce a catalytically active product especially useful in hydrocarbon conversion processes. Regardless of the cations present in the synthesized form of SSZ-42, the spatial arrangement of the atoms which form the basic crystal lattice of the zeolite remains essentially unchanged. The exchange of cations has little, if any effect on the zeolite lattice structure. SSZ-42 can be formed into a wide variety of physical shapes. Generally speaking, the zeolite can be in the form of a powder, a granule, or a molded product, such as extrudate having a particle size sufficient to pass through a 2-mesh (Tyler) screen and be retained on a 400-mesh (Tyler) screen. in cases where the catalyst is molded, such as by extrusion with an organic binder, the zeolite can be extruded before drying, or, dried or partially dried and then extruded. SSZ-42 can be composited with other materials resistant to the temperatures and other conditions employed in organic conversion processes. Such matrix materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and metal oxides. Examples of such materials and the manner in which they can be used are disclosed in United States Patent No. 4,910,006, issued May 20, 1990 to Zones et al., and copending U.S. Patent Application No. 959,205, filed October 9, 1992 entitled "ZEOLITE SSZ-35", both of which are incorporated by reference herein in their entirety. Hydrocarbon Conversion Processes SSZ-42 zeolites are useful in hydrocarbon conversion reactions. Hydrocarbon conversion reactions are chemical and catalytic processes in which carbon containing compounds are changed to different carbon containing compounds. Examples of hydrocarbon conversion reactions in which SSZ-42 are expected to be useful include catalytic cracking, hydrocracking, dewaxing, alkylation, and olefin and aromatics formation reactions. The catalysts are also expected to be useful in other petroleum refining and hydrocarbon conversion reactions such as isomerizing n-paraffins and naphthenes, polymerizing and oligomerizing olefinic or acetylenic compounds such as isobutylene and butene-1, reforming, alkylating, isomerizing polyalkyl substituted aromatics. (e.g. , -xylene) , and disproportionating aromatics (e.g., toluene) to provide mixtures of benzene, xylenes and higher methylbenzenes and oxidation reactions. The SSZ-42 catalysts have high selectivity, and under hydrocarbon conversion conditions can provide a high percentage of desired products relative to total products. SSZ-42 zeolites can be used in processing hydrocarbonaceous feedstocks. Hydrocarbonaceous feedstocks contain carbon compounds and can be from many different sources, such as virgin petroleum fractions, recycle petroleum fractions, shale oil, liquefied coal, tar sand oil, and, in general, can be any carbon containing fluid susceptible to zeolitic catalytic reactions. Depending on the type of processing the hydrocarbonaceous feed is to undergo, the feed can contain metal or be free of metals, it can also have high or low nitrogen or sulfur impurities. It can be appreciated, however, that in general processing will be more efficient (and the catalyst more active) the lower the metal, nitrogen, and sulfur content of the feedstock. The conversion of hydrocarbonaceous feeds can take place in any convenient mode, for example, in fluidized bed, moving bed, or fixed bed reactors depending on the types of process desired. The formulation of the catalyst particles will vary depending on the conversion process and method of operation. Other reactions which can be performed using the catalyst of this invention containing a metal, e.g., a Group VIII metal such platinum, include hydrogenation-dehydrogenation reactions, denitrogenation and desulfurization reactions. SSZ-42 can be used in hydrocarbon conversion reactions with active or inactive supports, with organic or inorganic binders, and with and without added metals. These reactions are well known to the art, as are the reaction conditions. Hydrocracking Using SSZ-42 catalyst which contains a hydrogenation promoter, heavy petroleum residual feedstocks, cyclic stocks and other hydrocrackate charge stocks can be hydrocracked using the process conditions and catalyst components disclosed in the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205. Typically, these feedstocks can be hydrocracked at hydrocracking conditions including a temperature in the range of from 175°C (347°F) to 485°C (905 β F), molar ratios of hydrogen to hydrocarbon charge from 1 to 100, a pressure in the range of from- 0.5 to 350 bar, and a liquid hourly space velocity (LHSV) in the range of from 0.1 to 30. The hydrocracking catalysts contain an effective amount of at least one hydrogenation component of the type commonly employed in hydrocracking catalysts. The hydrogenation component is generally selected from the group of hydrogenation catalysts consisting of one or more metals of Group VIB and Group VIII, including the salts, complexes and solutions containing such. The hydrogenation catalyst is preferably selected from the group of metals, salts and complexes thereof of the group consisting of at least one of platinum, palladium, rhodium, iridium and mixtures thereof or the group consisting of at least one of nickel, molybdenum, cobalt, tungsten, titanium, chromium and mixtures thereof. Reference to the catalytically active metal or metals is intended to encompass such metal or metals in the elemental state or in some form such as an oxide, sulfide, halide, carboxylate and the like. The hydrogenation catalyst is present in an effective amount to provide the hydrogenation function of the hydrocracking catalyst, and preferably in the range of from 0.05 to 25% by weight. Dewaxing SSZ-42 can be used to dewax hydrocarbonaceous feeds by selectively removing straight chain paraffins. The catalytic dewaxing conditions are dependent in large measure on the feed used and upon the desired pour point. Generally ' , the temperature will be between about 200°C (392 β F) and about 475 β C (887 β F) , preferably between about 250 β C (482 β F) and about 450°C (842 β F) . The pressure is typically between about 15 psig and about 3000 psig, preferably between about 200 psig and 3000 psig. The liquid hourly space velocity (LHSV) preferably will be from 0.1 to 20, preferably between about 0.2 and about 10. Hydrogen is preferably present in the reaction zone during the catalytic dewaxing process. The hydrogen to feed ratio is typically between about 500 and about 30,000 SCF/bbl (standard cubic feet per barrel) , preferably about 1000 to about 20,000 SCF/bbl. Generally, hydrogen will be separated from the product and recycled to the reaction zone. Typical feedstocks include light gas oil, heavy gas oils and reduced crudes boiling about 177 β C (350°F) . The SSZ- 2 hydrodewaxing catalyst may optionally contain a hydrogenation component of the type commonly employed in dewaxing catalysts. See the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205 for examples of these hydrogenation components. The hydrogenation component is present in an effective amount to provide an effective hydrodewaxing and hydroisomerization catalyst preferably in the range of from about 0.05 to 5% by weight. The catalyst may be run in such a mode to increase isodewaxing at the expense of cracking reactions. Aromatics Formation SSZ-42 can be used to convert light straight run naphthas and similar mixtures to highly aromatic mixtures. Thus, normal and slightly branched chained hydrocarbons, preferably having a boiling range above about 40°C (104°F) and less than about 300°C (572°F) , can be converted to products having a substantial higher octane aromatics content by contacting the hydrocarbon feed with the zeolite at a temperature in the range of from about 400°C (752°F) to 600 » C (1112°F), preferably 480 β C (896°F) to 550°C (1022°F) at pressures ranging from atmospheric to 10 bar, and liquid hourly space velocities (LHSV) ranging from 0.1 to 15. The conversion catalyst preferably contains a Group VIII metal compound to have sufficient activity for commercial use. By Group VIII metal compound as used herein is meant the metal itself or a compound thereof. The Group VIII noble metals and their compounds, platinum, palladium, and iridium, or combinations thereof can be used. Rhenium or tin or a mixture thereof may also be used in conjunction with the Group VIII metal compound and preferably a noble metal compound. The most preferred metal is platinum. The amount of Group VIII metal present in the conversion catalyst should be within the normal range of use in reforming catalysts, from about 0.05 to 2.0 weight percent, preferably 0.2 to 0.8 weight percent. it is critical to the selective production of aromatics in useful quantities that the conversion catalyst be substantially free of acidity, for example, by neutralizing the zeolite with a basic metal, e.g., alkali metal, compound. Methods for rendering the catalyst free of acidity are known in the art. See the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205 for a description of such methods. The preferred alkali metals are sodium, potassium, and cesium. The zeolite itself can be substantially free of acidity only at very high silica:alumina mole ratios; by "zeolite consisting essentially of silica" is meant a zeolite which is substantially free of acidity without base neutralization. Catalytic Cracking Hydrocarbon cracking stocks can be catalytically cracked in the absence of hydrogen using SSZ-42 at liquid hourly space velocities from 0.5 to 50, temperatures from about 127°C (260°F) to 885°C (1625°F) and pressures from subatmospheric to several hundred atmospheres, typically from about atmospheric to about 5 atmospheres. For this purpose, the SSZ-42 catalyst can be composited with mixtures of inorganic oxide supports as well as a traditional large pore crystalline cracking catalyst. As in the case of hydrocracking catalysts, when SSZ-42 is used as a catalytic cracking catalyst in the absence of hydrogen, the catalyst may be employed in conjunction with traditional cracking catalysts, e.g., any aluminosilicate heretofore employed as a component in cracking catalysts. Examples of these traditional cracking catalysts are disclosed in the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205. When a traditional cracking catalyst (TC) component is employed, the relative weight ratio of the TC to the SSZ-42 is generally between about 1:10 and about 500:1, desirably between about 1:10 and about 200:1, preferably between about 1:2 and about 50:1, and most preferably is between about 1:1 and about 20:1. The.cracking catalysts are typically employed with an inorganic oxide matrix component. See the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205 for examples of such matrix components. _r_ Oligomerization It is expected that SSZ-42 can also be used to oligomerize straight and branched chain olefins having from about 2 to 21 and preferably 2-5 carbon atoms. The oligomers which are the products of the process are medium to heavy olefins which are useful for both fuels, i.e., gasoline or a gasoline blending stock and chemicals. The oligomerization process comprises contacting the olefin feedstock in the gaseous state phase with SSZ-42 at a temperature of from about 232 β C (450°F) to about 649 β C (1200°F) , a LHSV of from about 0.2 to about 50 and a hydrocarbon partial pressure of from about 0.1 to about 50 atmospheres. Also, temperatures below about 232°C (450°F) may be used to oligomerize the feedstock, when the feedstock is in the liquid phase when contacting the zeolite catalyst. Thus, when the olefin feedstock contacts the zeolite catalyst in the liquid phase, temperatures of from about 10°C (50°F) to about 232°C (450 β F) , and preferably from 27°C (80°F) to 204 β C (400°F) may be used and a WHSV of from about 0.05 to 20 and preferably 0.1 to 10. It will be appreciated that the pressures employed must be sufficient to maintain the system in the liquid phase. As is known in the art, the pressure will be a function of the number of carbon atoms of the feed olefin and the temperature. Suitable pressures include from about 0 psig to about 3000 psig. The zeolite can have the original cations associated therewith replaced by a wide variety of other cations- according to techniques well known in the art. Typical cations would include hydrogen, ammonium and metal cations including mixtures of the same. Of the replacing metallic cations, particular preference is given to cations of metals such as rare earth metals, manganese, calcium, as well as metals of Group II of the Periodic Table, e.g., zinc, and Group VIII of the Periodic Table, e.g., nickel. One of the prime requisites is that the zeolite have a fairly low aromatization activity, i.e., in which the amount of aromatics produced is not more than about 20% by weight. This is accomplished by using a zeolite with controlled acid activity [alpha value] of from about 0.1 to about 120, preferably from about 0.1 to about 100, as measured by its ability to crack n-hexane. Alpha values are defined by a standard test known in the art, e.g., as shown in U.S. Patent No. 3,960,978 issued on June 1, 1976 to Givens, et al. which is incorporated totally herein by reference. If required, such zeolites may be obtained by steaming, by use in a conversion process or by any other method which may occur to one skilled in this art. SSZ-42 can be used to convert light gas C j - paraffins and/or olefins to higher molecular weight hydrocarbons including aromatic compounds. Operating temperatures of ιoθ β C (212 β F) to 700 β C (1292 β F) , operating pressures of 0 to 1000 psig and space velocities of 0.5-40 hr" 1 WHSV (weight hourly space velocity) can be used to convert the C j -C 6 paraffin and/or olefins to aromatic compounds. Preferably, the zeolite will contain a catalyst metal or metal oxide wherein said metal is selected from the group consisting of Groups IB, IIB, VIII and IIIA of the Periodic Table, and most preferably gallium or zinc and in the range of from about 0.05% to 5% by weight. Condensation of Alcohols SSZ-42 can be used to condense lower aliphatic alcohols having 1 to 10 carbon atoms to a gasoline boiling point hydrocarbon product comprising mixed aliphatic and aromatic hydrocarbon. The condensation reaction proceeds at a temperature of about 260°C (500°F) to 538 β C (1000°F) , a pressure of about 0.5 psig to 1000 psig and a space velocity of about 0.5 to 50 WHSV. The process disclosed in U.S. Patent No. 3,894,107 issued July 8, 1975 to Butter et al., describes the process conditions used in this process, which patent is incorporated totally herein by reference. The catalyst may be in the hydrogen form or may be base exchanged or impregnated to contain ammonium or a metal cation complement, preferably in the range of from about 0.05 to 5% by weight. The metal cations that may be present include any of the metals of the Groups I through VIII of the Periodic Table. However, in the case of Group IA metals, the cation content should in no case be so large as to effectively inactivate the catalyst. Isomerization The present catalyst is highly active and highly selective for isomerizing C 4 to C-, hydrocarbons. The activity means that the catalyst can operate at relatively low temperature which thermodynamically favors highly branched paraffins. Consequently, the catalyst can produce a high octane product. The high selectivity means that a relatively high liquid yield can be achieved when the catalyst is run at a high octane. 01 The present process comprises contacting the isomerization 02 catalyst with a hydrocarbon feed under isomerization 03 conditions. The feed is preferably a light straight run 04 fraction, boiling within the range of -1.1°C (30°F) to 121°C 05 (250?F) and preferably from 16°C (60°F) to 93 β C (200°F) . 06 Preferably, the hydrocarbon feed for the process comprises a 07 substantial amount of C to C- normal and slightly branched 08 low octane hydrocarbons, more preferably C s and C 6 09 hydrocarbons. 10 11 The pressure in the process is preferably between 50 psig 12 and 1000 psig, more preferably between 100 psig and 13 500 psig. The liquid hourly space velocity (LHSV) is 14 preferably between about 1 to about 10 with a value in the 15 range of about 1 to about 4 being more preferred. It is l β also preferable to carry out the isomerization reaction in 17 the presence of hydrogen. Preferably, hydrogen is added to 18 give a hydrogen to hydrocarbon ratio (H 2 /HC) of between 0.5 !• and 10 H 2 /HC, more preferably between 1 and 8 H 2 /HC. The 20 temperature is preferably between about 93 β C (200 β F) and 21 about 538 β C (1000 β F), more preferably between 204°C (400 β F) 22 and 316 β C (600 « F) . See the aforementioned U.S. Patent 2 3 No. 4,910,006 and U.S. Patent Application No. 959,205 for a 24 further discussion of isomerization process conditions. 25 * A low sulfur feed is especially preferred in the present 27 process. The feed preferably contains less than 10 ppm, 28 more preferably less than 1 ppm, and most preferably less 2' than 0.1 ppm sulfur. In the case of a feed which is not 30 already low in sulfur, acceptable levels can be reached by 31 hydrogenating the feed in a presaturation zone with a 32 hydrogenating catalyst which is resistant to sulfur 33 poisoning. See the aforementioned U.S. Patent No. 4,910,006 34 and U.S. Patent Application No. 959,205 for a further discussion of this hydrodesulfurization process. it is preferable to limit the nitrogen level and the water content of the feed. Catalysts and processes which are suitable for these purposes are known to those skilled in the art. After a period of operation, the catalyst can become deactivated by sulfur or coke. See the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent Application No. 959,205 for a further discussion of methods of removing this sulfur and coke, and of regenerating the catalyst. The conversion catalyst preferably contains a Group VIII metal compound to have sufficient activity for commercial use. By Group VIII metal compound as used herein is meant the metal itself or a compound thereof. The Group VIII noble metals and their compounds, platinum, palladium, and iridium, or combinations thereof can be used. Rhenium and tin may also be used in conjunction with the noble metal. The most preferred metal is platinum. The amount of Group VIII metal present in the conversion catalyst should be within the normal range of use in isomerizing catalysts, from about 0.05 to 2.0 weight percent, preferably 0.2 to o.8 weight percent. The .isomerization catalyst may also be calcined in a steam/air mixture at an elevated temperature after impregnation with the Group VIII metal, preferably platinum. Alkylation and Transalkylation SSZ-42 can be used in a process for the alkylation or transalkylation of an aromatic hydrocarbon. The process comprises contacting the aromatic hydrocarbon with a C-, to c 16 olefin alkylating agent or a polyalkyl aromatic hydrocarbon transalkylating agent, under at least partial liquid phase conditions, and in the presence of a catalyst comprising SSZ-42. SSZ-42 can also be used for removing benzene from gasoline by alkylating the benzene as described above and removing the alkylated product from the gasoline. For high catalytic activity, the SSZ-42 zeolite should be predominantly in its hydrogen ion form. Generally, the zeolite is converted to its hydrogen form by ammonium exchange followed by calcination. If the zeolite is synthesized with a high enough ratio of organo-nitrogen cation to sodium ion, calcination alone may be sufficient. It is preferred that, after calcination, at least 80% of the cation sites are occupied by hydrogen ions and/or rare earth ions. The pure SSZ-42 zeolite may be used as a catalyst, but generally it is preferred to mix the zeolite powder with an inorganic oxide binder such as alumina, silica, silica/alumina, or naturally occurring clays and form the mixture into tablets or extrudates.. The final catalyst may contain from 1 to 99 weight percent SSZ-42 zeolite. Usually the zeolite content will range from 10 to 90 weight percent, and more typically from 60 to 80 weight percent. The• preferred inorganic binder is alumina. The mixture may be formed into tablets or extrudates having the desired shape by methods well known in the art. Examples of suitable aromatic hydrocarbon feedstocks which may be alkylated or transalkylated by the process of the invention include aromatic compounds such as benzene, toluene and xylene. The preferred aromatic hydrocarbon is benzene. Mixtures of aromatic hydrocarbons may also be employed. Suitable olefins for the alkylation of the aromatic hydrocarbon are those containing 2 to 20, preferably 2 to 4, carbon atoms, such as ethylene, propylene, butene-1, trans-butene-2 and cis-butene-2, or mixtures thereof. The preferred olefin is propylene. These olefins may be present in admixture with the corresponding C^ to C^, paraffins, but it is preferable to remove any dienes, acetylenes, sulfur compounds or nitrogen compounds which may be present in the olefin feedstock stream, to prevent rapid catalyst deactivation. Longer chain alpha olefins may be used as well. when transalkylation is desired, the transalkylating agent is a polyalkyl aromatic hydrocarbon containing two or more alkyl groups that each may have from 2 to about 4 carbon atoms. For example, suitable polyalkyl aromatic hydrocarbons include di-, tri- and tetra-alkyl aromatic hydrocarbons, such as diethylbenzene, triethylbenzene, • diethylmethylbenzene (diethyltoluene) , di-isopropylbenzene, di-isopropyltoluene, dibutylbenzene, and the like. Preferred polyalkyl aromatic hydrocarbons are the dialkyl benzenes. A particularly preferred polyalkyl aromatic hydrocarbon is di-isopropylbenzene. When alkylation is the process conducted, reaction conditions are as follows. The aromatic hydrocarbon feed should be present in stoichiometric excess. It is preferred that molar ratio of aromatics to olefins be greater than four-to-one to prevent rapid catalyst fouling. The reaction temperature may range from 38 β C (100°F) to 316°C (600°F) , preferably 121* (250 β F) to 232 β C (450°F) . The reaction pressure should be sufficient to maintain at least a partial liquid phase in order to retard catalyst fouling. This is typically 50 psig to 1000 psig depending on the feedstock and reaction temperature. Contact time may range from ιo seconds to 10 hours, but is usually from 5 minutes to an hour. The weight hourly space velocity (WHSV) , in terms of grams (pounds) of aromatic hydrocarbon and olefin per gram (pound) of catalyst per hour, is generally within the range of about 0.5 to 50. When transalkylation is the process conducted, the molar ratio of aromatic hydrocarbon will generally range from about 1:1 to 25:1, and preferably from about 2:1 to 20:1. The reaction temperature may range from about 38°C (100°F) to 316 β C (600 β F), but it is preferably about 121°C (250 β F) to 232°C (450*F). The reaction pressure should be sufficient to maintain at least a partial liquid phase, typically in the range of about 50 psig to 1000 psig, preferably 300 psig to 600 psig. The weight hourly space velocity will range from about 0.1 to 10. U.S. Patent No. 5,082,990 issued on January 21, 1992 to Hsieh, et al. describes such processes and is incorporated herein by reference. SSZ-42 can also be used as an adsorbent with high selectivities based on molecular sieve behavior and also based upon preferential hydrocarbon packing within the pores. Xylene Isomerization SSZ-42 may also be useful in a process for isomerizing one or more xylene isomers in a C 8 aromatic feed to obtain ortho-, meta- and para-xylene in a ratio approaching the equilibrium value. In particular, xylene isomerization is used in conjunction with a separation process to manufacture para-xylene. For example, a portion of the para-xylene in a mixed C, aromatics stream may be recovered by crystallization and centrifugation. The mother liquor from the crystallizer is then reacted under xylene isomerization conditions to restore ortho-, meta- and para-xylenes to a near equilibrium ratio. At the same time, part of the ethylbenzene in the mother liquor is converted to xylenes or to products which are easily separated by distillation. The isomerate is blended with fresh feed and the combined stream is distilled to remove heavy and light by-products. The resultant C, aromatics stream is then sent to the crystallizer to repeat the cycle. EXAMPLES The following examples demonstrate but do not limit the present invention. Example 1 Synthesis of N-benzyl-l,4-diazabicyclo[2.2.2]octane cation 145 Grams of l,4-diazabicyclo[2.2.2]octane (commonly referred to as "DABCO") was dissolved in 2.5 liters of ethyl acetate and chilled to 0°C (32 β F). 209 Grams of benzyl bromide was added dropwise while the chilled solution was stirred. Caution should be exercised because the reaction is rapid and requires cooling. The product was collected by filtration and recrystallized from a minimum of warm methanol. The recrystallized product gave a microanalysis and NMR pattern consistent with the 1:1 adduct. The quaternary ammonium compound was ion exchanged using hydroxide exchange resin AG1-X8 from BioRad. The exchanged solution was titrated for molarity and the yield of exchange was greater than 90%. The resulting compound was designated Template A. Example 2 Synthesis of l-azabicyclo[2.2.2]octane cation The procedure of Example 1 was repeated using the same molar quantity of 1-azabicyclo[2.2.2]octane (commonly referred to as "quinuclidine") as the DABCO in Example 1. This compound was designated Template B. Example 3 The procedure of Example 1 was repeated using the same molar quantity of 3-hydroxy-l-azabicyclo[2.2.2]octane in place of the DABCO. The resulting compound was designated Template C. Example 4 Synthesis of SSZ-42 3 Millimoles of Template A as a 5.5 ml aqueous solution was used to dissolve 0.06 gram sodium borate decahydrate, and 0.6 gram Cabosil M5 silica was slurried into the resulting solution. The reaction mixture was heated in a Teflon cup of a stainless steel reactor at 150°C (302°F) for 17 days without agitation. A crystalline product formed which was isolated and identified as SSZ-42 by its X-ray diffraction (XRD) pattern. Examples 5-11 Synthesis of SSZ-42 Procedures similar to that of Example 4 was used to prepare SSZ-42 using the materials and amounts shown in Table C below. 01 02 03 04 05 06 07 08 09 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 Example 12 Calcination of SSZ-42 The crystalline product of Example 11 was subjected to calcination as follows. The sample was heated in a muffle furnace from room temperature to 600°C (1112°F) in stages and under a stream of nitrogen with a very small air bleed. The stages were to 125°C (257°F) at 50 β C (122°F)/hr, hold for two hours, 50 β C (122 β F)/hr to 540°C (1004°F) , hold for four hours, 50 β C (122 β F)/hr to 600 β C (1112 β F) with a final hold for four hours. The micropore volume for nitrogen of the sample was determined to be 0.20 cc/g and a BET surface area of 470 m 2 /g was calculated for this material, demonstrating that SSZ-42 is a highly microporous material. Example 13 ion Exchange of Calcined SSZ-42 ion exchange of calcined SSZ-42 was carried out using a 1/1/20 mass ratio of SSZ-42/ammonium acetate/water, with the mixture being heated at 95°C (203°F) for two hours. After cooling, the exchanged zeolite was filtered and washed with water. The resulting product was analyzed and had the XRD data shown in Table IV below. 01 02 03 04 05 06 07 08 09 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 2Theta d LO_- 35.241 2.5447 0.8 35.599 2.5199 2.4 36.240 2.4768 1.9 36.759 2.4430 2.9 Example 14 Preparation of Aluminosilicate SSZ-42 The aluminosilicate form of SSZ-42 was made from the product of Example 12. 92 Grams of the borosilicate product of Example 12 was added to 1200 cc water and 101.2 grams of aluminum nitrate nonahydrate in the liner of a 2 liter autoclave. The reactor was sealed and heated at 140°C (284°F) without stirring for 3 days, and the resulting zeolite was filtered for recovery and washed with water. The resulting product was analyzed and found to have the XRD lines shown in Table V below. 1 TABLE V 2 03 04 05 06 07 08 09 10 11 12 3 14 15 16 17 18 19 20 21 22 23 24 25 26 27 Constraint Index Determination 28 29 0.50 Gram of 20-40 mesh granules (after pelletization to 3000 psi and pellet breakup) of the product of Example 14 3 311 wwaass ppaacckkeedd iinnttoo aa 11//44 iinncchh ssttaaiinnlleessss sstteeeell rreeaaccttoorr ttuubbee ww:ith 32 alundum on both sides of the zeolite bed. The reactor was 3 3 3 3 placed in a Lindburg furnace and heated to 540°C (1004°F) 34 for drying. At l25 β C (257 β F) helium was introduced into the reactor at lOcc/minute and atmospheric pressure. The temperature was gradually raised to 280°C (536°F) over 40 minutes. Feed was introduced by means of a syringe pump at a rate of 0.62 cc/hr of a 50/50 (v/v) mixture of n-hexane and 3-methylpentane. Direct sampling onto a gas chromatograph was begun at ten minutes. This first point showed an overall conversion of 70% and a Constraint Index calculated at 0.65. Large pore behavior in cracking was observed. Example 16 Preparation of Gallosilicate SSZ-42 5.1 Grams of the product of Example 13 was mixed with 4.85 grams of gallium nitrate nonahydrate and 82 cc of water. The resulting mixture was heated in a polypropylene bottle for 3 days at 95°C (203°F) and then filtered and washed to yield the gallosilicate form of SSZ-42. The resulting product was analyzed and found to have the XRD lines shown in Table VI below. Methanol Conversion to Higher Hydrocarbons The catalyst as prepared in Examples 14 and 15 was tested ffoorr ccoonnvveerrssiioonn ooff mmeetthhaannooll.. AA ddoowwnnffllooww rreeaaccttoorr,, ssyyrriinge pump and on-line gas chromatograph were used for the reaction. At 400°C (752°F) and 5 minutes on stream, the conversion of methanol is 100%, and the following hydrocarbons were analyzed in area percent: it can be seen that there is considerable hydrogen transfer early in the reaction for this very active and acidic zeolite. Also, the selectivities are indicative of at least one large pore system. Example 18 Preparation of Cesium-neutralized, Platinum SSZ-42 SSZ-42 (10.00 grams, moisture-free) was mixed with 80.00 grams de-ionized water. A solution of 7.00 grams CsOH (66,450 ppm Cs) in 23 grams de-ionized water was then added to the catalyst slurry and shaken for 24 hours. The pH after exchange was 9.8. The catalyst was filtered and air dried for 72 hours. It was then dried at l2l β C (250°F) for 16 hours and then calcined in air at 299°C (570°F) for 2 hours. The calcined Cs-SSZ-42 was mixed with 80.00 grams de-ionized water and 30.00 grams of a solution of platinumtetraamine dichloride in de-ionized water was added to the mixture. The resulting catalyst slurry was shaken for 18 hours. It was then filtered and air dried to constant moisture. The air dried catalyst was further dried at 121 β C (250°F) for 16 hours and then calcined in air at 299°C (570°F) for 2 hours. The finished catalyst had 4 wt% Cs and 0.5 wt% Pt. The cyclohexane micropore volume of the finished catalyst was 0.133 cc/grams and the Pt dispersion calculated from hydrogen adsorption was 72%. Example 19 Reforming to Benzene Using SSZ-42 Catalyst The cesium neutralized, platinum SSZ-42 catalyst of Example 18 (0.45 gram) was tested in a small pilot plant at 130 psig, 3.0 weight hourly space velocity, 3.0 hydrogen to hydrocarbon molar ratio and once-through hydrogen. The hydrocarbon feed was 149°C (300°F) end point naphtha of the following composition: 67 wt% paraffins 24 wt% naphthenes 9 wt% aromatics Catalyst temperature was adjusted to maintain a 95 research octane target. The performance of this catalyst was compared to a commercial reforming catalyst and the results are shown in Table D below. 1 Based on feed. The results in Table D show that SSZ-42 catalyst can be prepared with high activity and high aromatics selectivity while being used at low operating pressure. The remarkable stability of the SSZ-42 catalyst is shown in the drawing. There, run hours versus temperature are plotted for a reaction similar to that described in Example 19. The reactions were carried out at 3.0 WHSV, 3.0 H 2 :hydrocarbon and using a light naptha feed (149°C (300°F) end point) . The plots shown in the drawing are as follows: Example 20 Preparations of SSZ-42 SSZ-42 was prepared as described in Example 4, except that one-half of the sodium borate was replaced with sodium aluminate trihydrate. After 6 days at 150°C (302°F) , the recovered product was SSZ-42. The lattice constants for the diffraction lines indicated a shift to a larger unit cell, consistent with aluminum incorporation into the product (as is also seen in Example 14) . Example 21 Preparation of FCC Catalyst A modified form of FCC catalyst can be prepared from SSZ-42 and used in MAT testing. 4 Grams of Catapal alumina (solids basis) was peptized with 0.8 grams formic acid in 40 ml water. 22 Grams of kaolin (solids basis) was mixed in and processed in a blender. 10 Grams of Al-SSZ-42, from Example 14 was mixed in 20 ml water and this mixture was subsequently also blended in. After blending, this catalyst mixture was dried at 120°C (248°F) overnight. Next the solids were meshed to 100-325 and then calcined by placing in an oven already at 600°C (1112°F) (3 hours of calcination) . λ comparable comparative catalyst was made from Y zeolite (using CBV 500 from PQ Corporation) . A blank was made by making one more catalyst where kaolin replaced the amount of zeolite used in the preparation. Example 22 Testing of SSZ-42 (Fresh) in FCC Application MAT testing was carried out with a 3.2 Catalyst/Oil ratio, a 75 second contact time and at 530 β C (986 β F) using a FCC feed. The data for the three prepared materials from Example 21 is given in Table E below. TABLE E Kaolin blank Wt% Conv. 220°C 23 (428 β F) minus Coke 2.9 Hydrogen 0.3 Methane 0.5 Ethane 0.4 Ethylene 0.3 Propane 0.3 Propylene 0.7 Isobutane 0.1 n-Butane 0.1 Isobutene 0.4 Total butenes 0.8 Pentenes 0.4 Gasoline 16.8 It can be seen that the fresh SSZ-42 composited catalyst shows useful conversion of FCC feed, and in particular, makes a high slate of useful gas products (such as isobutane and olefins) as well as gasoline.

Claims: WHAT IS CLAIMED IS: 1. A zeolite having a mole ratio of an oxide selected from silicon oxide, germanium oxide and mixtures thereof to an oxide selected from aluminum oxide, gallium oxide, iron oxide, titanium oxide, boron oxide and mixtures thereof greater than about 10 and having the X-ray diffraction lines of Table I. 2. A zeolite according to Claim 1 wherein the oxides comprise silicon oxide and aluminum oxide. 3. A zeolite according to Claim 1 wherein the oxides comprise silicon oxide and boron oxide. 4. The zeolite of Claim 3 wherein the boron in said zeolite in excess of 100 parts per million is replaced by at least one other element in a post-synthesis treatment. 5. The zeolite of Claim 4 wherein the replacing element is a Group IIIA metal or a first row transition metal. 6. The zeolite of Claim 5 wherein the replacing element is aluminum, chromium, gallium, iron, silicon, titanium, zinc, or mixtures thereof. 7.. The zeolite of Claim 6 wherein the replacing element is aluminum. 8. A zeolite having a composition, as-synthesized and in the anhydrous state, in terms of mole ratios as follows: 01 Y0 2 /W 2 0 J Greater than or equal to 15 02 YO 2 /M 2 O Greater than or equal to 45 03 Y0 2 /Q 10-40 04 05 wherein Q is comprised of cations selected from the 08 group consisting of N- 07 benzyl-l,4-diazabicyclo[2.2.2Joctane cations and 08 N-benzyl-l-azabicyclo[2.2.2]octane cations, M is an 0 ' alkali metal cation or alkaline earth metal cation, W 10 is a trivalent atom selected from the group consisting 11 of boron, aluminum, gallium, iron, titanium, and 12 mixtures thereof wherein at least 50% of W is boron, 1 3 and Y is selected from the group consisting of silicon, 14 germanium, and mixtures thereof, said zeolite having 15 the X-ray diffraction lines of Table I. 16 17 9. A zeolite having a mole ratio of an oxide selected from 18 silicon oxide, germanium oxide and mixtures thereof to 1' an oxide selected from aluminum oxide, gallium oxide, 20 iron oxide, titanium oxide, boron oxide and mixtures 21 thereof greater than about 10 and having, after 22 calcination, the X-ray diffraction lines of Table II. 23 24 10. A zeolite according to Claim 9 wherein the oxides 25 comprise silicon oxide and aluminum oxide. 26 27 11. λ zeolite according to Claim 9 wherein the oxides 28 comprise silicon oxide and boron oxide. 29 30 12. A zeolite according to Claim 9, wherein said zeolite is 31 in the hydrogen form. 32 33 13. A zeolite according to Claim 10, wherein said zeolite 3.4 is in the hydrogen form. 14. A zeolite according to Claim 11, wherein said zeolite is in the hydrogen form. 15. A zeolite having an average pore size diameter greater than about 6 Angstroms and having the X-ray diffraction lines of Table II. 16. A catalyst comprising the zeolite of Claim 12. 17. A catalyst comprising the zeolite of Claim 13. 18. A catalyst comprising the zeolite of Claim 14. 19. A catalyst according to Claim 16 wherein the zeolite is substantially free of acidity. 20. A catalyst according to Claim 17 wherein the zeolite is substantially free of acidity. 21. A catalyst according to Claim 18 wherein the zeolite is substantially free of acidity. 22. A process for converting hydrocarbons comprising contacting a hydrocarbonaceous feed at hydrocarbon converting conditions with the catalyst of Claim 16. 23. λ hydrocracking process comprising contacting a hydrocarbon feedstock under hydrocracking conditions with the catalyst of Claim 16. 24. A dewaxing process comprising contacting a hydrocarbon feedstock under dewaxing conditions with the catalyst of Claim 16. 25. A process for increasing the octane of a hydrocarbon feedstock to produce a product having an increased aromatics content comprising contacting a hydrocarbonaceous feedstock which comprises normal and slightly branched hydrocarbons having a boiling range above about 40°C and less than about 300°C, under aromatic conversion conditions with the catalyst of Claim 19. 26. The process of Claim 25 wherein the catalyst contains a Group VIII metal component. 27. A process for converting heavy paraffinic and naphthenic feedstocks boiling between about 200°C and about 300°C to lighter aromatics under aromatic conversion conditions with the catalyst of Claim 19. 28. The process of Claim 27 wherein the catalyst contains a Group VIII metal component. 29. A catalytic cracking process comprising contacting a hydrocarbon feedstock in a reaction zone under catalytic cracking conditions in the absence of added hydrogen with a catalyst comprising the zeolite of Claim 12. 30. The process of Claim 29 wherein the catalyst additionally comprises a large pore crystalline cracking component. 31. The process of Claim 30 wherein the catalyst composition comprises a physical mixture of the two components. 1 32. The process of Claim 31 wherein the two catalyst 2 components are incorporated in an inorganic matrix. 3 4 33. An isomerizing process for isomerizing C 4 to C- 5 hydrocarbons, comprising contacting a catalyst, 6 comprising at least one Group VIII metal and the 7 catalyst of Claim 16, with a feed having normal and 8 slightly branched C 4 to C-, hydrocarbons under ' isomerizing conditions. 0 1 34. The process of Claim 33 wherein the catalyst has been 2 calcined in a steam/air mixture at an elevated 3 temperature after impregnation of the Group VIII metal. 4 5 35. The process of Claim 34 wherein the Group VIII metal is 8 platinum. 7 8 36. A process for alkylating an aromatic hydrocarbon which 8 comprises contacting under alkylation conditions at 0 least a mole excess of an aromatic hydrocarbon with a 1 C-j to C M olefin under at least partial liquid phase 2 conditions and in the presence of the catalyst of 3 Claim 16. 4 5 37. The process of Claim 36 wherein the olefin is a C_> to C 4 * olefin. 7 8 38. The process of Claim 36 wherein the aromatic 9 hydrocarbon and olefin are present in a molar ratio of 0 about 4:1 to about 20:1, respectively. 1 2 3 4 39. The process of Claim 38 wherein the aromatic hydrocarbon is selected from the group consisting of benzene, toluene, xylene, or mixtures thereof. 40. A process for transalkylating an aromatic hydrocarbon which comprises contacting under transalkylating conditions an aromatic hydrocarbon with a polyalkyl aromatic hydrocarbon under at least partial liquid phase conditions and in the presence of the catalyst of Claim 16. 41. The process of Claim 40 wherein the aromatic hydrocarbon and the polyalkyl aromatic hydrocarbon are present in a molar ratio of from about 1:1 to about 25:1, respectively. 42. The process of Claim 40 wherein the aromatic hydrocarbon is a member selected from the group consisting of benzene, toluene, xylene, or mixtures thereof. 43. The process of Claim 40 wherein the polyalkyl aromatic hydrocarbon is a dialkylbenzene. 44. λ process to convert paraffins to aromatics which comprises contacting paraffins with the catalyst of Claim 16, said catalyst comprising gallium, zinc, or a compound of gallium or zinc, 45. A process for converting lower alcohols and other oxygenated hydrocarbons comprising contacting said lower alcohol or other oxygenated hydrocarbon with the catalyst of Claim 16 under conditions to produce liquid products. 46. A process for isomerizing olefins comprising contacting said olefin with the catalyst of Claim 16 under conditions which cause isomerization of said olefin. 47. A process for isomerizing an isomerization feed containing an aromatic C, stream of ethylbenzene or xylene isomers or mixtures thereof, wherein a more nearly equilibrium ratio of ortho-, meta- and para- xylenes is obtained, said process comprising contacting said feed under isomerization conditions with the catalyst of Claim 12.

Inventors: RAINIS ANDREW, ZONES STACEY I, RAINIS, ANDREW, ZONES, STACEY, I.
Applicants: CHEVRON USA INC, CHEVRON U.S.A. INC.
Application year: 1995
Main classification: C01B33
IPC codes: B01J29, C01B39, C07C2, C07C5, C07C6, C10G3, C10G11, C10G35, C10G45, C10G47, C10G50