ZEOLITE SSZ-44

Abstract: The present invention relates to new crystalline zeolite SSZ-44 prepared by processes for preparing crystalline molecular sieves, particularly large pore zeolites, using an N,N-diethyl-cis-2,6-dimethyl piperidinium cation templating agent.

Description: 1 ZEOLITE SSZ-44 2 3 The present invention relates to new crystalline zeolite SSZ-44, a method for preparing 4 SSZ-44 using a N,N-diethyi-cis-2,6-dimethyl piperidinium cation templating agent, and 5 processes employing SSZ-44 as a catalyst. 6 Because of their unique sieving characteristics, as well as their catalytic 07 properties, crystalline molecular sieves are especially useful in applications such as g hydrocarbon conversion, gas drying and separation Although many different Q crystalline molecular sieves have been disclosed, there is a continuing need for new , Q zeolites with desirable properties for gas separation and drying, hydrocarbon and . , chemical conversions, and other applications New zeolites may contain novel internal 12 pore architectures, providing enhanced selectivities in these processes A vanety of templates have been used to synthesize a variety of molecular 13 sieves, including zeolites ofthe silicate, aluminosilicate, and borosilicate families 14 However, the specific zeolite which may be obtained by using a given template is at 15 present unpredictable 16 The present invention is directed to a family of crystalline molecular sieves with 17 unique properties, referred to herein as "zeolite SSZ-44" or simply "SSZ-44". 18 Preferably SSZ-44 is obtained in its silicate, aluminosilicate, titanosilicate, 19 vanadosilicate or borosilicate form The term "silicate" refers to a zeolite having a 0 high mole ratio of silicon oxide relative to aluminum oxide, preferably a mole ratio 1 greater than 100 As used herein the term "aluminosilicate" refers to a zeolite 2 containing both alumina and silica and the term "borosilicate" refers to a zeolite 3 containing oxides of both boron and silicon 4 In accordance with the present invention, there is provided a zeolite having an 5 average pore size greater than about 6 Angstroms and having the X-ray diffraction 6 lines of Table I 7 in accordance with this invention there is also provided a zeolite having a mole 8 ratio of an oxide of a first tetravalent element to an oxide of a second trivalent or 9 tetravalent element different from said first tetravalent element, said mole ratio being 0 greater than about 20 and having the X-ray diffraction lines of Table I 1 Further in accordance with this invention there is provided a zeolite having a 2 mole ratio of an oxide selected from silicon oxide, germanium oxide and mixtures 3 thereof to an oxide selected from aluminum oxide, gallium oxide, iron oxide, boron 4 oxide, titanium oxide, indium oxide, vanadium oxide and mixtures thereof greater than 1 about 20 and having the X-ray diffraction lines of Table I below. The present 2 invention further provides such a zeolite having a composition, as synthesized and in 3 the anhydrous state, in terms of mole ratios as follows: 5 M7YO 2 < 0.05 6 Q YO 2 0.01 - 0.10 7 where Q comprises a N,N-diethyl-cis-2,6-dimethyl piperidinium cation; M is an alkali g metal cation; W is selected from the group aluminum, gallium, iron, boron, titanium, 9 indium, vanadium and mixtures thereof; a = 1 or 2, b = 2 when a is 1 (i.e., W is j 0 tetravalent) and b = 3 when a is 2 (i.e., W is trivalent); and Y is selected from the j j group consisting of silicon, germanium and mixtures thereof. 12 In accordance with this invention, there is also provided a zeolite prepared by 13 thermally treating 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, 14 gallium oxide, iron oxide, boron oxide, titanium oxide, indium oxide, vanadium oxide 15 and mixtures thereof greater than about 20 and having the X-ray diffraction lines of 16 Table I at a temperature of from about 200°C to about 800°C, the thus-prepared 17 zeolite having the X-ray diffraction lines of Table II. The present invention also 18 includes this thus-prepared zeolite which is predominantly in the hydrogen form, which 19 hydrogen form is prepared by ion exchanging with an acid or with a solution of an 0 ammonium salt followed by a second calcination. In accordance with the present 1 invention there is also provided a catalyst comprising the zeolite of this invention 22 predominantly in the hydrogen form. 3 Further provided in accordance with this invention is a catalyst comprising the 4 zeolite of this invention made substantially free of acidity by neutralizing said zeolite ith a basic metal. 6 Also provided in accordance with the present invention is a method of 27 preparing a crystalline material comprising one or a combination of oxides selected 28 from the group consisting of oxides of one or more tetravalent element(s) and one or 29 more trivalent element(s), said method comprising contacting under crystallization 30 conditions sources of said oxides and a templating agent comprising a N,N-diethyl-cis- 31 2,6-dimethyl piperidinium cation. 32 The present invention additionally provides a process for converting 33 hydrocarbons comprising contacting a hydrocarbonaceous feed at hydrocarbon 34 converting conditions with a catalyst comprising the zeolite of this invention. 1 Further provided by the present invention is a hydrocracking process comprising contacting a hydrocarbon feedstock under hydrocracking conditions with a 3 catalyst comprising the zeolite of this invention, preferably predominantly in the 4 hydrogen form. 5 This invention also includes a dewaxing process comprising contacting a 6 hydrocarbon feedstock under dewaxing conditions with a catalyst comprising the 7 zeolite of this invention, preferably predominantly in the hydrogen form. g Also included in this invention is a process for increasing the octane of a 9 hydrocarbon feedstock to produce a product having an increased aromatics content 0 comprising contacting a hydrocarbonaceous feedstock which comprises normal and , slightly branched hydrocarbons having a boiling range above about 40°C and less than η about 200°C, under aromatic conversion conditions with a catalyst comprising the zeolite of this invention made substantially free of acidity by neutralizing said zeolite 3 with a basic metal. Also provided in this invention is such a process wherein the 4 zeolite contains a Group VIII metal component. 5 Also provided by the present invention is a catalytic cracking process 6 comprising contacting a hydrocarbon feedstock in a reaction zone under catalytic 7 cracking conditions in the absence of added hydrogen with a catalyst comprising the 8 zeolite of this invention, preferably predominantly in the hydrogen form. Also included 9 in this invention is such a catalytic cracking process wherein the catalyst additionally 0 comprises a large pore crystalline cracking component. 1 The present invention further provides an isomerizing process for isomerizing C 4 to C 7 hydrocarbons, comprising contacting a catalyst, comprising at least one 3 Group VIII metal and the zeolite of this invention, preferably predominantly in the hydrogen form, with a feed having normal and slightly branched C to C 7 hydrocarbons 5 under isomerizing conditions. Also provided is such an isomerization process wherein 6 the catalyst has been calcined in a steam/air mixture at an elevated temperature after 7 impregnation ofthe Group VIII metal, preferably platinum. 8 This invention also provides a process for alkylating an aromatic hydrocarbon 9 which comprises contacting under alkylation conditions at least a mole excess of an 0 aromatic hydrocarbon with a C 2 to C 2 o olefin under at least partial liquid phase 1 conditions and in the presence of a catalyst comprising the zeolite of this invention, preferably predominantly in the hydrogen form. This invention additionally provides 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 a catalyst compπsing the zeolite of this invention, preferably predominantly in the hydrogen form Further provided by this invention is a process to convert paraffins to aromatics which comprises contacting paraffins with a catalyst co pnsing the zeolite of this invention, preferably predominantly in the hydrogen form, said catalyst comprising gallium, zinc, or a compound of gallium or zinc This invention also provides a process for converting lower alcohols and other oxygenated hydrocarbons comprising contacting said lower alcohol or other oxygenated hydrocarbon with a catalyst compnsing the zeolite of this invention, preferably predominantly in the hydrogen form, under conditions to produce liquid products Further provided in accordance with this invention is a process for isomenzing an isomenzation feed comprising an aromatic Cg stream of xylene isomers or mixtures of xylene isomers and ethylbenzene, wherein a more nearly equilibπum ratio of ortho-, meta and para-xylenes is obtained, said process comprising contacting said feed under isomenzation conditions with a catalyst comprising the zeolite of this invention, preferably predominantly in the hydrogen form The present invention further provides a process for oligomerizing olefins comprising contacting an olefin feed under oligomerization conditions with a catalyst compnsing the zeolite of this invention, preferably predominantly in the hydrogen form Also provided by the present invention is an improved process for the reduction of oxides of nitrogen contained in a gas stream in the presence of oxygen wherein said process comprises contacting the gas stream with a zeolite, the improvement comprising using as the zeolite a zeolite having a mole ratio of an oxide of a first tetravalent element to an oxide of a second tetravalent trivalent element different from said first tetravalent element, said mole ratio being greater than about 20 and having the X-ray diffraction lines of Table I The zeolite may contain a metal or metal ions capable of catalyzing the reduction ofthe oxides of nitrogen, and may be conducted , the presence of a stoichiometric excess of oxygen In a preferred embodiment, the gas stream is the exhaust stream of an internal combustion engine DETAILED DESCRIPTION OF THE INVENTION The present invention compnses a family of crystalline, large pore zeolites, SSZ-44 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 In preparing SSZ-44 zeolites, a N,N-diethyl-cis-2,6-dimethyl piperidinium cation is used as a crystallization template In general, SSZ-44 is prepared by contacting an active source of one or more oxides selected from the group consisting of monovalent element oxides, divalent element oxides, trivalent element oxides, and tetravalent element oxides with the N,N-diethyl-cis-2,6-dimethyl piperidinium cation templating agent (seen as "Q" below). SSZ-44 is prepared from a reaction mixture having the composition shown in Table A below TABLE A - Reaction Mixture Typical Preferred YO 2 /W,Ob 20 and greater 25 and greater OH- YO 2 0.1 to 0.5 0 15 to 0 40 Q/YO 2 0 05 to 0.40 0 10 to 0.30 M+ YO 2 0 05 to 0.40 0 05 to 0.30 H 2 O/YO 2 15 to 100 20 to 50 where Y, W, a, b, Q and M are as defined above In practice, SSZ-44 is prepared by a process comprising (a) preparing an aqueous solution containing sources of at least one oxide capable of forming a crystalline molecular sieve and a N,N-diethyl-cis-2,6- dimethyl piperidinium cation having an anionic counterion which is not detrimental to the formation of SSZ-44, (b) maintaining the aqueous solution under conditions sufficient to form crystals of SSZ-44, and (c) recovering the crystals of SSZ-44 Accordingly, SSZ-44 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 of a first tetravalent element(s), and one or a combination of a second trivalent or tetravalent element(s) different from the first tetravalent element(s) The first tetravalent element(s) is preferably selected from the group consisting of silicon, germanium and combinations thereof, more preferably silicon The second trivalent or tetravalent element (which is different from the first tetravalent element) is preferably 1 selected from the group consisting of aluminum, gallium, iron, boron, titanium, indium, 2 vanadium and combinations thereof, more preferably aluminum, boron or titanium. 3 Typical sources of aluminum oxide for the reaction mixture include aluminates, 4 alumina, aluminum colloids, aluminum oxide coated on silica sol, hydrated alumina gels 5 such as Al(OH)j and aluminum compounds such as AIC1 3 and Al 2 (SO ) 3 . Typical 6 sources of silicon oxide include silicates, silica hydrogel, silicic acid, fumed silica, 7 colloidal silica, tetra-alkyl orthosilicates, and silica hydroxides. Boron, as well as g gallium, germanium, titanium, indium, vanadium and iron can be added in forms 9 corresponding to their aluminum and silicon counterparts. 10 A source zeolite reagent may provide a source of aluminum or boron. In most , , cases, the source zeolite also provides a source of silica. The source zeolite in its 12 dealuminated or deboronated form may also be used as a source of silica, with additional silicon added using, for example, the conventional sources listed above. Use 13 of a source zeolite reagent as a source of alumina for the present process is more 14 completely described in U.S. Patent No. 4,503,024 issued on March 5, 1985 to 15 Bourgogne, the disclosure of which is incoφorated herein by reference. 16 Typically, an alkali metal hydroxide and/or an alkaline earth metal hydroxide, 17 such as the hydroxide of sodium, potassium, lithium, cesium, rubidium, calcium, and 18 magnesium, is used in the reaction mixture; however, this component can be omitted 19 so long as the equivalent basicity is maintained. The templating agent may be used to 0 provide hydroxide ion. Thus, it may be beneficial to ion exchange, for example, the 21 halide for hydroxide ion, thereby reducing or eliminating the alkali metal hydroxide 22 quantity required. The alkali metal cation or alkaline earth cation may be part ofthe as-synthesized crystalline oxide material, in order to balance valence electron charges 24 therein. 25 The reaction mixture is maintained at an elevated temperature until the crystals 2 ofthe SSZ-44 zeolite are formed. The hydrotherma! crystallization is usually 27 conducted under autogenous pressure, at a temperature between 100°C and 200°C, 28 preferably between 135° and 180°C. The crystallization period is typically greater than 29 1 day and preferably from about 3 days to about 20 days. Preferably the zeolite is 30 prepared using mild stirring or agitation. 31 During the hydrothermal crystallization step, the SSZ-44 crystals can be 32 allowed to nucleate spontaneously from the reaction mixture. The use of SSZ-44 33 crystals as seed material can be advantageous in decreasing the time necessary for 34 complete crystallization to occur. In addition, seeding can lead to an increased purity 1 ofthe product obtained by promoting the nucleation and/or formation of SSZ-44 over 02 any undesired phases. When used as seeds, SSZ-44 crystals are added in an amount 03 between 0.1 and 10% ofthe weight of silica used in the reaction mixture. 04 Once the zeolite crystals have formed, the solid product is separated from the 05 reaction mixture by standard mechanical separation techniques such as filtration. The 6 crystals are water-washed and then dried, e.g., at 90°C to 150°C for from 8 to 24 07 hours, to obtain the as-synthesized SSZ-44 zeolite crystals. The drying step can be g performed at atmospheric pressure or under vacuum. 9 SSZ-44 as prepared has a mole ratio of an oxide selected from silicon oxide, 10 germanium oxide and mixtures thereof to an oxide selected from aluminum oxide, , , gallium oxide, iron oxide, boron oxide, titanium oxide, indium oxide, vanadium oxide 12 and mixtures thereof greater than about 20; and has the X-ray diffraction lines of Table I below. SSZ-44 further has a composition, as synthesized and in the anhydrous state, 13 in terms of mole ratios, shown in Table B below. 14 TABLE B - As-Svnthesized SSZ-44 15 YO 2 /W,O b > 20 (preferably, 20 to about 400) 16 M7YO 2 < 0.05 (preferably, about 0.00005 - 0.05) 17 Q/YO 2 0.01 - 0.10 18 where Y, W, a, b, M and Q are as defined above. 19 SSZ-44 can be made essentially aluminum free, i.e., having a silica to alumina 0 mole ratio of ∞. The term "essentially alumina-free" means that no aluminum is 1 intentionally added to the reaction mixture, e.g., as an alumina or aluminate reagent, 2 and that to the extent aluminum is present, it occurs only as a contaminant in the 3 reagents. An additional method of increasing the mole ratio of silica to alumina is by 4 using standard acid leaching or chelating treatments. SSZ-44 can also be prepared 5 directly as either an aluminosilicate or a borosilicate. Lower silica to alumina ratios may be obtained by using methods which insert 7 aluminum into the crystalline framework. For example, aluminum insertion may occur 8 by thermal treatment ofthe zeolite in combination with an alumina binder or dissolved 9 source of alumina. Such procedures are described in U.S. Patent 4,559,315, issued on 0 December 17, 1985 to Chang, et al. 1 It is believed that SSZ-44 is comprised of a new framework structure or 2 topology which is characterized by its X-ray diffraction pattern. SSZ-44 zeolites, 3 as-synthesized, have a crystalline structure whose X-ray powder diffraction pattern 4 exhibit the characteristic lines shown in Table I an 1 is thereby distinguished from other known zeolites. TABLE I - As-Svnthesized SSZ-44 2 Theta d Relative Intensity (l) 7.7 1 1.4 M 8.0 1 1.0 VS 8.7 10.2 M 16.0 5.6 M 19.0 4.6 VS 19.6 4.5 M 20.5 4.3 M 21.6 4.1 M 23.7 3.8 M 25.5 3.5 S (i) The X-ray patterns provided are based on a relative intensity scale in which the strongest line in the X-ray pattern is assigned a value of 100: W(weak) is less than 20; M(medium) is between 20 and 40; S(strong) is between 40 and 60; VS(very strong) is greater than 60. After calcination, the SSZ-44 zeolites have a crystalline structure whose X-ray powder diffraction pattern include the characteristic lines shown in Table II: TABLE II - Calcined SSZ-44 2 Theta d Relative Intensity 7.7 11.4 M-S 8.0 1 1.0 VS 8.7 10.2 S-VS 16.0 5.5 VV 19.2 4.6 M 19.6 4.5 VV 20.5 4.3 VV 21.6 4.1 VV 23.8 3.7 VV 25.6 3.5 VV The X-ray powder diffraction patterns were determined 1 ry standard techniques. The radiation was the K-alpha/doublet of copper. The peak heights and the positions, 1 as a function of 2Θ where θ is the Bragg angle, were read from the relative intensities 2 of the peaks, and d, the interplanar spacing in Angstroms corresponding to the 3 recorded lines, can be calculated. The variation in the scattering angle (two theta) 4 measurements, due to instrument error and to differences between individual samples, 5 is estimated at +/- 0.20 degrees. 6 Minor variations in the diffraction pattern can result from variations in the 7 silica-to-alumina or silica-to-boron mole ratio of the particular sample due to changes g in lattice constants. In addition, sufficiently small crystals will affect the shape and 9 intensity of peaks, leading to significant peak broadening. JO Calcination can also result in changes in the intensities of the peaks as , compared to patterns ofthe "as-made" material, as well as minor shifts in the , - diffraction pattern. The zeolite produced by exchanging the metal or other cations present in the zeolite with various other cations (such as H + or NH ) yields essentially 13 the same diffraction pattern, although again, there may be minor shifts in the 14 interplanar spacing and variations in the relative intensities of the peaks. 15 Notwithstanding these minor perturbations, the basic crystal lattice remains unchanged 16 by these treatments. 17 Crystalline SSZ-44 can be used as- synthesized, but preferably will be thermally 18 treated (calcined). Usually, it is desirable to remove the alkali metal cation by ion 19 exchange and replace at least part of it with hydrogen, ammonium, or any desired 0 metal ion. The zeolite can be leached with chelating agents, e.g., EDTA or dilute acid 1 solutions, to increase the silica to alumina mole ratio. The zeolite can also be steamed; 2 steaming helps stabilize the crystalline lattice to attack from acids. 3 The zeolite can be used in intimate combination with hydrogenating 4 components, such as tungsten, vanadium molybdenum, rhenium, nickel cobalt, chromium, manganese, or a noble metal, such as palladium or platinum, for those 6 applications in which a hydrogenation-dehydrogenation function is desired. 7 Metals may also be introduced into the zeolite by replacing some of the cations 8 in the zeolite with metal cations via standard ion exchange techniques (see, for 9 example, U.S. Patent Nos. 3, 140,249 issued on July 7, 1964 to Plank, et al.; 3, 140,251 0 issued on July 7, 1964 to Plank, et al.; and 3, 140,253 issued on July 7, 1964 to Plank, 1 et al ). Typical replacing cations can include metal cations, e.g., rare earth, Group IA, 2 Group II A and Group VIII metals, as well as their mixtures. Ofthe replacing metallic 3 cations, cations of metals such as rare earth, Mn, Ca, Mg, Zn, Cd, Pt, Pd, Ni, Co, Ti, 4 Al, Sn, and Fe are particularly preferred. 01 The hydrogen, ammonium, and metal components can be ion-exchanged into 2 the SSZ-44. The zeolite can also be impregnated with the metals, or, the metals can be 3 physically and intimately admixed with the zeolite using standard methods known to 4 the art. 5 Regardless ofthe cations present in the synthesized form of SSZ-44, the spatial 6 arrangement ofthe atoms which form the basic crystal lattice ofthe zeolite remains 7 essentially unchanged 8 SSZ-44 can be composited with other materials resistant to the temperatures 9 and other conditions employed in organic conversion processes Such matrix materials JO 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 U S Patent No 13 5,316,753, issued May 31, 1994 to Nakagawa, both of which are incorporated by 14 reference herein in their entirety 15 Hydrocarbon Conversion Processes 16 SSZ-44 zeolites are useful in hydrocarbon conversion reactions Hydrocarbon 17 conversion reactions are chemical and catalytic processes in which carbon containing 18 compounds are changed to different carbon containing compounds Examples of 19 hydrocarbon conversion reactions in which SSZ-44 are expected to be useful include 20 catalytic cracking, hydrocracking, dewaxing, alkylation, and olefin and aromatics 1 formation reactions The catalysts are also expected to be useful in other petroleum 2 refining and hydrocarbon conversion reactions such as isomerizing n-paraffins and 3 naphthenes, polymerizing and oiigomerizing olefinic or acetylenic compounds such as 24 isobutylene and butene- 1, reforming, alkylating (including alkylation of aromatics by other hydrocarbons), isomerizing polyalkyl substituted aromatics (e g , m-xylene), and 2 6 disproportionating aromatics (e.g , toluene) to provide mixtures of benzene, xylenes 27 and higher methylbenzenes and oxidation reactions Also included are rearrangement 28 reactions to make various naphthalene derivatives The SSZ-44 catalysts have high 29 selectivity, and under hydrocarbon conversion conditions can provide a high 30 percentage of desired products relative to total products 31 SSZ-44 zeolites can be used in processing hydrocarbonaceous feedstocks 32 Hydrocarbonaceous feedstocks contain carbon compounds and can be from many 33 different sources, such as virgin petroleum fractions, recycle petroleum fractions, shale 34 oil, liquefied coal, tar sand oil, synthetic paraffins from NAO, recycled plastic feedstocks and, in general, can be any carbon containing feedstock 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 ofthe 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 ofthe 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 VTII metal such platinum, include hydrogenation-dehydrogenation reactions, denitrogenation and desulfuπzation reactions The following table indicates typical reaction conditions which may be employed when using catalysts comprising SSZ-44 in the hydrocarbon conversion reactions of this invention Preferred conditions are indicated in parentheses Process Temp , °C Pressure LHSV Hydrocracking 175-485 0 5-350 bar 0 1-30 Dewaxing 200-475 15-3000 psig 0 1-20 (250-450) (200-3000) (0 2-10) Aromatics formation 400-600 atm -10 bar 0 1-15 (480-550) Cat cracking 127-885 subat -' 0 5-50 (atm -5atm ) Oligomenzation 232-649 2 0 1-50 atm w 0 2-50 2 10-232 4 0 05-20 5 (27-204) 4 (0 1-10) 5 Paraffins to 100-700 0-1000 psig 0 5-40 5 aromatics Condensation of 260-538 0 5-1000 psig 0 5-50 5 alcohols 1 Several hundred atmospheres 2 Gas phase reaction 3 Hydrocarbon partial pressure 4 Liquid phase reaction 5 VVHSV Other reaction conditions and parameters are provided below. Hydrocracking Using a catalyst which comprises SSZ-44 in the hydrogen form and 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 No. 5,316,753. The hydrocracking catalysts contain an effective amount of at least one hydrogenation component ofthe 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 VTB 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, ruthenium 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 ofthe hydrocracking catalyst, and preferably in the range of from 0.05 to 25% by weight. Dewaxing SSZ-44 in the hydrogen form can be used to dewax hydrocarbonaceous feeds by selectively removing straight chain paraffins. Typically, the viscosity index ofthe 01 dewaxed product is improved (compared to the waxy feed) when the waxy feed is 02 contacted with SSZ-44 under isomerization dewaxing conditions. 03 The catalytic dewaxing conditions are dependent in large measure on the feed 04 used and upon the desired pour point. Hydrogen is preferably present in the reaction 05 zone during the catalytic dewaxing process. The hydrogen to feed ratio is typically 06 between about 500 and about 30,000 SCF/bbl (standard cubic feet per barrel), 07 preferably about 1000 to about 20,000 SCF/bbl. Generally, hydrogen will be separated øg from the product and recycled to the reaction zone. Typical feedstocks include light 0 gas oil, heavy gas oils and reduced crudes boiling above about 350°F. 0 A typical dewaxing process is the catalytic dewaxing of a hydrocarbon oil , , feedstock boiling above about 350°F and containing straight chain and slightly 12 branched chain hydrocarbons by contacting the hydrocarbon oil feedstock in the presence of added hydrogen gas at a hydrogen pressure of about 15-3000 psi with a 13 catalyst comprising SSZ-44 and at least one group VTII metal. 14 The SSZ-44 hydrodewaxing catalyst may optionally contain a hydrogenation 15 component ofthe type commonly employed in dewaxing catalysts. See the 16 aforementioned U.S. Patent No. 4,910,006 and U.S. Patent No. 5,316,753 for 17 examples of these hydrogenation components. 18 The hydrogenation component is present in an effective amount to provide an 19 effective hydrodewaxing and hydroisomerization catalyst preferably in the range of 20 from about 0.05 to 5% by weight. The catalyst may be run in such a mode to increase 21 isodewaxing at the expense of cracking reactions. 22 The feed may be hydrocracked, followed by dewaxing. This type of two stage 23 process and typical hydrocracking conditions are described in U.S. Patent 4 No. 4,921,594, issued May 1, 1990 to Miller, which is incoφorated herein by 25 reference in its entirety. 2 SSZ-44 may also be utilized as a dewaxing catalyst in the form of a layered 27 catalyst. That is, the catalyst comprises a first layer comprising zeolite SSZ-44 and at 28 least one Group VIII metal, and a second layer comprising an aluminosilicate zeolite 29 which is more shape selective than zeolite SSZ-44. The use of layered catalysts is 30 disclosed in U.S. Patent No. 5, 149,421, issued September 22, 1992 to Miller, which is 3 1 incoφorated by reference herein in its entirety. The layering may also include a bed of 2 SSZ-44 layered with a non-zeolitic component designed for either hydrocracking or 33 hydrofinishing. 34 01 SSZ-44 may also be used to dewax raffinates, including bright stock, under 02 conditions such as those disclosed in U. S. Patent No. 4,181,598, issued January 1, 03 1980 to Gillespie et al., which is incoφorated by reference herein in its entirety. 04 It is often desirable to use mild hydrogenation (sometimes referred to as 05 hydrofinishing) to produce more stable dewaxed products. The hydrofinishing step 06 can be performed either before or after the dewaxing step, and preferably after. 07 Hydrofinishing is typically conducted at temperatures ranging from about 190°C to øg about 340°C at pressures from about 400 psig to about 3000 psig at space velocities 09 (LHSV) between about 0.1 and 20 and a hydrogen recycle rate of about 400 to 1500 10 SCF/bbl. The hydrogenation catalyst employed must be active enough not only to , , hydrogenate the olefins, diolefins and color bodies which may be present, but also to 12 reduce the aromatic content. Suitable hydrogenation catalyst are disclosed in U. S 13 Patent No. 4,921,594, issued May 1, 1990 to Miller, which is incoφorated by reference herein in its entirety. The hydrofinishing step is beneficial in preparing an 14 acceptably stable product (e.g., a lubricating oil) since dewaxed products prepared 15 from hydrocracked stocks tend to be unstable to air and light and tend to form sludges 16 spontaneously and quickly. 17 Lube oil may be prepared using SSZ-44. For example, a C 20 + lube oil may be made 18 by isomerizing a C 2 o+ olefin feed over a catalyst comprising SSZ-44 in the hydrogen 19 form and at least one Group VIII metal. Alternatively, the lubricating oil may be made 20 by hydrocracking in a hydrocracking zone a hydrocarbonaceous feedstock to obtain an 21 effluent comprising a hydrocracked oil, and catalytically dewaxing the effluent at a 22 temperature of at least about 400°F and at a pressure of from about 15 psig to about J 3000 psig in the presence of added hydrogen gas with a catalyst comprising SSZ-44 in the hydrogen form and at least one Group VIII metal. 2 5 Aromatics Formation 26 SSZ-44 can be used to convert light straight run naphthas and similar mixtures 27 to highly aromatic mixtures. Thus, normal and slightly branched chained 28 hydrocarbons, preferably having a boiling range above about 40°C and less than about 29 200°C, can be converted to products having a substantial higher octane aromatics 30 content by contacting the hydrocarbon feed with a catalyst comprising SSZ-44. It is 31 also possible to convert heavier feeds into BTX or naphthalene derivatives of value 32 using SSZ-44-containing catalysts. 33 The conversion catalyst preferably contains a Group VIII metal compound to 34 have sufficient activity for commercial use. By Group VIII metal compound as used 01 herein is meant the metal itself or a compound thereof The Group VIII noble metals 02 and their compounds, platinum, palladium, and iridium, or combinations thereof can be 03 used Rhenium or tin or a mixture thereof may also be used in conjunction with the 04 Group VIII metal compound and preferably a noble metal compound. The most 05 preferred metal is platinum The amount of Group VIII metal present in the 06 conversion catalyst should be within the normal range of use in reforming catalysts, 07 from about 0 05 to 2 0 weight percent, preferably 0.2 to 0 8 weight percent. øg It is critical to the selective production of aromatics in useful quantities that the 09 conversion catalyst be substantially free of acidity, for example, by neutralizing the j 0 zeolite with a basic metal, e g., alkali metal, compound. Methods for rendering the j , catalyst free of acidity are known in the art. See the aforementioned U.S Patent , „ No 4,910,006 and U S Patent No 5,316,753 for a description of such methods The preferred alkali metals are sodium, potassium, rubidium and cesium The 13 zeolite itself can be substantially free of acidity only at very high silica: alumina mole 14 ratios 15 Catalytic Cracking 16 Hydrocarbon cracking stocks can be catalytically cracked in the absence of 17 hydrogen using SSZ-44 in the hydrogen form. 18 When SSZ-44 is used as a catalytic cracking catalyst in the absence of 19 hydrogen, the catalyst may be employed in conjunction with traditional cracking 20 catalysts, e g , any aluminosilicate heretofore employed as a component in cracking 21 catalysts Typically, these are large pore, crystalline aluminosilicates Examples of 22 these traditional cracking catalysts are disclosed in the aforementioned U S. Patent 23 No 4,910,006 and U.S. Patent No 5,316,753 When a traditional cracking catalyst 24 (TC) component is employed, the relative weight ratio ofthe TC to the SSZ-44 is 2 5 generally between about 1 : 10 and about 500 1, desirably between about 1 10 and 2 about 200 1, preferably between about 1.2 and about 50 1, and most preferably is 27 between about 1 1 and about 20 1 The zeolite and/or traditional cracking component 28 may be further ion exchanged with rare earth ions to modify selectivity 29 The cracking catalysts are typically employed with an inorganic oxide matrix 30 component See the aforementioned U.S Patent No 4,910,006 and U.S. Patent 31 No 5,316,753 for examples of such matrix components 32 Oligomerization 33 It is expected that SSZ-44 in the hydrogen form can also be used to 34 ohgomerize straight and branched chain olefins having from about 2 to 21 and „„„„,,,„ PCT/US96/I8588 WO 97/20769 -16- 1 preferably 2-5 carbon atoms The oligomers which are the products ofthe process are 2 medium to heavy olefins which are useful for both fuels, l e , gasoline or a gasoline 3 blending stock and chemicals 4 The oligomerization process comprises contacting the olefin feedstock in the 5 gaseous or liquid phase with a catalyst comprising SSZ-44 6 The zeolite can have the onginal cations associated therewith replaced by a 7 wide vanety of other cations according to techniques well known in the art Typical g cations would include hydrogen, ammonium and metal cations including mixtures of 9 the same Ofthe replacing metallic cations, particular preference is given to cations of j 0 metals such as rare earth metals, manganese, calcium, as well as metals of Group II of j , the Peπodic Table, e g , zinc, and Group VIII ofthe Penodic Table, e g , nickel One 12 ofthe prime requisites is that the zeolite have a fairly low aromatization activity, i e , in 13 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 14 about 0 1 to about 120, preferably from about 0 1 to about 100, as measured by its 15 ability to crack n-hexane 16 Alpha values are defined by a standard test known in the art, e g , as shown in 17 U S Patent No 3,960,978 issued on June 1, 1976 to Givens, et al which is 18 incoφorated totally herein by reference If required, such zeolites may be obtained by 19 steaming, by use in a conversion process or by any other method which may occur to 0 one skilled in this art 1 Conversion of Paraffins to Aromatics 2 SSZ-44 in the hydrogen form can be used to convert light gas C 2 -C 6 paraffins 3 to higher molecular weight hydrocarbons including aromatic compounds Preferably, 4 the zeolite will contain a catalyst metal or metal oxide wherein said metal is selected from the group consisting of Group IB, IIB, VIII and IIIA of the Penodic Table 6 Preferably, the metal is gallium, niobium, indium or zinc in the range of from about 7 0 05 to 5% by weight 8 Condensation of Alcohols 9 SSZ-44 can be used to condense lower aliphatic alcohols having 1 to 10 carbon 0 atoms to a gasoline boiling point hydrocarbon product compnsing mixed aliphatic and 1 aromatic hydrocarbon The process disclosed in U S Patent No 3,894, 107 issued 2 July 8, 1975 to Butter et al , descπbes the process conditions used in this process, 3 which patent is incorporated totally herein by reference 4 WO 97/20769 -17- 1 The catalyst may be in the hydrogen form or may be base exchanged or 2 impregnated to contain ammonium or a metal cation complement, preferably in the 3 range of from about 0.05 to 5% by weight. The metal cations that may be present 4 include any ofthe metals ofthe Groups I through VIII of the Periodic Table 5 However, in the case of Group IA metals, the cation content should in no case be so 6 large as to effectively inactivate the catalyst, nor should the exchange be such to 7 eliminate all acidity. There may be other processes involving treatment of oxygenated g substrates where a basic catalyst is desired 9 Isomerization j 0 The present catalyst is highly active and highly selective for isomerizing C to 11 C 7 hydrocarbons. The activity means that the catalyst can operate at relatively low temperature which thermodynamically favors highly branched paraffins Consequently, 12 the catalyst can produce a high octane product The high selectivity means that a 13 relatively high liquid yield can be achieved when the catalyst is run at a high octane 14 The present process comprises contacting the isomerization catalyst, i.e., a 15 catalyst comprising SSZ-44 in the hydrogen form, with a hydrocarbon feed under 16 isomerization conditions The feed is preferably a light straight run fraction, boiling 17 within the range of 30°F to 250°F and preferably from 60°F to 200°F Preferably, the 18 hydrocarbon feed for the process comprises a substantial amount of C to C 7 normal 19 and slightly branched low octane hydrocarbons, more preferably C? and Ct, 0 hydrocarbons 1 It is preferable to carry out the isomerization reaction in the presence of 2 hydrogen Preferably, hydrogen is added to give a hydrogen to hydrocarbon ratio 3 (H 2 /HC) of between 0.5 and 10 H 2 /HC, more preferably between 1 and 8 H 2 /HC See 4 the aforementioned U.S. Patent No 4,910,006 and U S Patent No 5,316,753 for a 5 further discussion of isomerization process conditions 6 A low sulfur feed is especially preferred in the present process The feed preferably contains less than 10 ppm, more preferably less than 1 ppm, and most 8 preferably less than 0.1 ppm sulfur In the case of a feed which is not already low in 9 sulfur, acceptable levels can be reached by hydrogenating the feed in a presaturation 0 zone with a hydrogenating catalyst which is resistant to sulfur poisoning See the 1 aforementioned U S. Patent No 4,910,006 and U.S Patent No 5,316,753 for a 2 further discussion of this hydrodesulfurization process 3 4 01 It is preferable to limit the nitrogen level and the water content ofthe feed. 2 Catalysts and processes which are suitable for these puφoses are known to those 3 skilled in the art. 4 After a period of operation, the catalyst can become deactivated by sulfur or 5 coke. See the aforementioned U.S. Patent No. 4,910,006 and U.S. Patent 6 No. 5,316,753 for a further discussion of methods of removing this sulfur and coke, 7 and of regenerating the catalyst. 0g The conversion catalyst preferably contains a Group VIII metal compound to 0 have sufficient activity for commercial use. By Group VIII metal compound as used JO herein is meant the metal itself or a compound thereof. The Group VIII noble metals j , and their compounds, platinum, palladium, and iridium, or combinations thereof can be . r. used. Rhenium and tin may also be used in conjunction with the noble metal. The 13 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, 14 from about 0.05 to 2.0 weight percent, preferably 0.2 to 0.8 weight percent. 15 Alkylation and Transalkylation 16 SSZ-44 can be used in a process for the alkylation or transalkylation of an 17 aromatic hydrocarbon. The process comprises contacting the aromatic hydrocarbon 18 with a C 2 to C)6 olefin alkylating agent or a polyalkyl aromatic hydrocarbon 19 transalkylating agent, under at least partial liquid phase conditions, and in the presence 0 of a catalyst comprising SSZ-44. 1 SSZ-44 can also be used for removing benzene from gasoline by alkylating the 2 benzene as described above and removing the alkylated product from the gasoline. 3 For high catalytic activity, the SSZ-44 zeolite should be predominantly in its 24 hydrogen ion form. It is preferred that, after calcination, at least 80% ofthe cation sites are occupied by hydrogen ions and/or rare earth ions. Examples of suitable aromatic hydrocarbon feedstocks which may be alkylated 7 or transalkylated by the process of the invention include aromatic compounds such as 8 benzene, toluene and xylene. The preferred aromatic hydrocarbon is benzene. There 29 may be occasions where naphthalene derivatives may be desirable. Mixtures of 30 aromatic hydrocarbons may also be employed. 31 Suitable olefins for the alkylation of the aromatic hydrocarbon are those 32 containing 2 to 20, preferably 2 to 4, carbon atoms, such as ethylene, propylene, 33 butene- 1, trans-butene-2 and cis-butene-2, or mixtures thereof. There may be 34 1 instances where pentenes are desirable. The preferred olefins are ethylene and 2 propylene. Longer chain alpha olefins may be used as well. 3 When transalkylation is desired, the transalkylating agent is a polyalkyl 4 aromatic hydrocarbon containing two or more alkyl groups that each may have from 2 5 to about 4 carbon atoms. For example, suitable polyalkyl aromatic hydrocarbons 6 include di-, tri- and tetra-alkyl aromatic hydrocarbons, such as diethylbenzene, 7 triethylbenzene, diethylmethylbenzene (diethyltoluene), di-isopropylbenzene, g di-isopropyltoluene, dibutylbenzene, and the like. Preferred polyalkyl aromatic hydrocarbons are the dialkyi benzenes. A particularly preferred polyalkyl aromatic j 0 hydrocarbon is di-isopropylbenzene. j , When alkylation is the process conducted, reaction conditions are as follows. 12 The aromatic hydrocarbon feed should be present in stoichiometric excess. It is 13 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 100°F to 600°F, 14 preferably 250°F to 450°F. The reaction pressure should be sufficient to maintain at 15 least a partial liquid phase in order to retard catalyst fouling. This is typically 50 psig 16 to 1000 psig depending on the feedstock and reaction temperature. Contact time may 17 range from 10 seconds to 10 hours, but is usually from 5 minutes to an hour. The 18 weight hourly space velocity (VVHSV), in terms of grams (pounds) of aromatic 19 hydrocarbon and olefin per gram (pound) of catalyst per hour, is generally within the 0 range of about 0.5 to 50. 1 When transalkylation is the process conducted, the molar ratio of aromatic 2 hydrocarbon will generally range from about 1 : 1 to 25: 1, and preferably from about 3 2:1 to 20: 1. The reaction temperature may range from about 100°F to 600°F, but it is 4 preferably about 250°F to 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 6 1000 psig, preferably 300 psig to 600 psig. The weight hourly space velocity will 7 range from about 0.1 to 10. U.S. Patent No. 5,082,990 issued on January 21, 1992 to 8 Hsieh, et al. describes such processes and is incoφorated herein by reference. 9 Xylene Isomerization 0 SSZ-44 in the hydrogen form may also be useful in a process for isomerizing 1 one or more xylene isomers in a Cs aromatic feed to obtain ortho-, meta-, and para- 2 xylene in a ratio approaching the equilibrium value. In particular, xylene isomerization 3 is used in conjunction with a separate process to manufacture para-xylene. For 4 example, a portion ofthe para-xylene in a mixed Cg aromatics stream may be 01 recovered by crystallization and centrifugation. The mother liquor from the crystallizer 02 is then reacted under xylene isomerization conditions to restore ortho-, meta- and 03 para-xylenes to a near equilibrium ratio. At the same time, part ofthe ethylbenzene in 04 the mother liquor is converted to xylenes or to products which are easily separated by 05 filtration. The isomerate is blended with fresh feed and the combined stream is distilled 06 to remove heavy and light by-products. The resultant Cg aromatics stream is then sent 07 to the crystallizer to repeat the cycle. Og Optionally, isomerization in the vapor phase is conducted in the presence of 3.0 09 to 30.0 moles of hydrogen per mole of alkylbenzene (e.g., ethylbenzene). If hydrogen j 0 is used, the catalyst should comprise about 0.1 to 2.0 wt% of a j j hydrogenation/dehydrogenation component selected from Group VIII (of the Periodic , „ Table) metal component, especially platinum or nickel. By Group VIII metal component is meant the metals and their compounds such as oxides and sulfides. 13 Optionally, the isomerization feed may contain 10 to 90 wt% of a diluent such 14 as toluene, trimethylbenzene, naphthenes or paraffins. 15 Other Uses for SSZ-44 16 SSZ-44 can also be used as an adsorbent with high selectivities based on 17 molecular sieve behavior and also based upon preferential hydrocarbon packing within 18 the pores. 19 SSZ-44 may also be used for the catalytic reduction of the oxides of nitrogen in 20 a gas stream. Typically the gas stream also contains oxygen, often a stoichiometric 21 excess thereof. Also, the SSZ-44 may contain a metal or metal ions within or on it 22 which are capable of catalyzing the reduction of the nitrogen oxides. Examples of such 23 metals or metal ions include copper, cobalt and mixtures thereof. 24 One example of such a process for the catalytic reduction of oxides of nitrogen 2 in the presence of a zeolite is disc. >„.ed in U.S. Patent No. 4,297,328, issued 6 October 27, 1981 to Ritscher et al., which is incoφorated by reference herein. There, 27 the catalytic process is the combustion of carbon monoxide and hydrocarbons and the 28 catalytic reduction of the oxides of nitrogen contained in a gas stream, such as the 29 exhaust gas from an internal combustion engine. The zeolite used is metal ion- 30 exchanged, doped or loaded sufficiently so as to provide an effective amount of 3 1 catalytic copper metal or copper ions within or on the zeolite. In addition, the process 32 is conducted in an excess of oxidant, e.g., oxygen. 33 EXAMPLES 34 The following examples demonstrate but do not limit the present invention. 01 Example 1 02 Synthesis of N.N-diethyl-cis-2.6-dimethylpiperidinium 03 hydroxide (Template A) 04 Thirty-six grams of cis-2,6-dimethylpiperidine was mixed with 320 ml of 05 methanol and 64 grams of potassium bicarbonate. Ethyl iodide (199 grams) was added 06 dropwise to the reaction mixture and, following complete addition, the reaction was 07 heated at reflux for three days. Following isolation ofthe desired product, the salt was øg recrystallized from hot acetone and ether with a small amount of methanol and the 09 iodide salt was converted to the hydroxide salt by treatment with Bio-Rad AG1-X8 , o anion exchange resin. The hydroxide ion concentration was determined by titration of , , the resulting solution using phenolphthalein as the indicator. , ,., Example 2 Preparation of Aluminosilicate SSZ-44 13 Starting SiO ? /Al ? θ = 100 14 Four grams of a solution of Template A (0.56 mmol OFT/g) was mixed with 15 6.4 grams of water and 1.5 grams of 1.0 N NaOH. Reheis F2000 hydrated aluminum 16 hydroxide (0.029 gram) was added to this solution and, following complete dissolution 17 of the solid, 0.92 gram of Cabosil M-5 fumed silica was added. The resulting reaction 18 mixture was sealed in a Parr 4745 reactor and heated at 170°C and rotated at 43 φm. 19 After seven days, a settled product was obtained and determined by XRD to be 20 SSZ-44. Analysis of this product showed the SiO 2 /Al 2 Oj mole ratio to be 80. 21 Representative X-ray diffraction data for the product appears in Table III below. In 22 table III and subsequent tables, the intensity of each peak is expressed as 100 x I I 0 , 23 where lo is the intensity ofthe strongest line or peak. 24 5 6 7 8 9 0 1 2 3 4 TABLE III 2 Theta d lOOxI/Iø 2 Theta d l OxI/I, 7.70 11.48 23.3 23.30 3.82 11.0 8.01 11.03 82.7 23.48 3.79 6.5 8.68 10.18 32.3 23.71 3.75 28.8 12.59 7.03 7.6 24.38 3.65 18.2 15.31 5.78 17.5 24.66 3.61 28.8 15.92 5.56 24.8 24.82 3.58 27.0 16.98 5.22 5.4 25.06 3.55 32.6 17.84 4.97 10.2 25.50 3.49 46.5 19.11 4.64 100.0 26.22 3.40 15.2 19.64 4.52 30.0 26.98 3.30 22.2 20.06 4.42 4.2 27.60 3.23 10.5 20.45 4.34 26.3 28.42 3.14 9.7 20.18 4.19 7.4 28.80 3.10 6.2 21.59 4.1 1 18.0 29.56 3.02 5.6 21.91 4.05 8.6 29.81 2.99 4.6 22.38 3.97 5.5 30.93 2.89 5.5 Example 3 Preparati on of Aluminos licate SSZ-44 Starting $iQ 2 /Al 2 C > 3 = 100 Four grams of a solution of Template A (0.56 mmol OHVg) was mixed with 4.3 grams of water and 1.5 grams of 1.0 N NaOI i. Reheis F2000 (0.029 gram) was added to this solution and, following complete di ssolution ofthe solid, 3.0 grams of Ludox AS-30 (DuPont) aqueous colloidal silica was added. This mixture was heated at 170°C and rotated at 43 φm for 12 days, after which a settled product was obtained. Analysis by XRD showed the product to be SSZ-44. Example A Seeded Preparation of Alum inosilicate SSZ-44 The reaction described in Example 2 was repeated, with the exception of seeding with 0.006 gram of SSZ-44 crystals. In this case, SSZ-44 was » obtained in five days. Example 5 Preparation of Aluminosilicate SSZ-44 Starting S ty/Al-tOi = 67 The reaction as described in Example 4 was repeated, with the exception of using 0 044 gram of Reheis F2000 silica in the reaction mixture This resulted in a SiO 2 /Al 2 O 3 mole ratio in the reaction mixture of 67 After six days at 170°C (43 φm) a product was isolated and determined by X-ray diffraction data to be SSZ-44 X-ray diffraction data for this product appears in Table IV below TABLE IV 2 Theta d lOOxI/In 2 Theta d lOOxI/In 7.78 1137 28 2170 4096 22 806 10.97 84 2194 4051 13 8.72 1014 29 2244 3962 5 12.62 701 8 2340 3802 14 13.74 645 4 2376 3745 36 15.32 567 19 2444 3642 22 15.98 5.55 22 2512 3545 34 1704 520 5 2558 3483 42 1794 495 13 2570 3463 25 1916 4632 100 2626 3394 15 1968 4511 33 2702 3300 20 20.22 4392 6 2764 3227 11 2050 4332 26 2848 3134 13 21.28 4175 8 3104 2881 5 3366 2663 10 Example 6 Preparation of Aluminosilicate SSZ-44 Starting SiO 2 /Al 2 Oτ ~ 50 The reaction described in Example 2 was repeated, with the exception that 0 058 gram of Reheis F2000 was used This resulted in a starting SiO 2 /AJ Oι mole ratio of 50 After 1 1 days at 170°C and 43 φm a product was isolated and determined by XRD to be SSZ-44 The product was analyzed and found to have a SiO 2 /Al 2 O 3 mole ratio of 51 01 Example 7 02 Preparation of Aluminosilicate SSZ-44 03 Starting SiO ? /Al 7 O, = 40 04 The reaction described in Example 2 was repeated, with the exception that 05 0.073 gram of Reheis F2000 was used. This resulted in a starting Siθ 2 /Al 2 θ 3 mole 06 ratio of 40. After 11 days at 170°C and 43 φm a product was isolated and determined 07 by XRD to be SSZ-44. Analysis of this product gave a SiO 2 /Al 2 O 3 mole ratio of 38. øg Example 8 09 Preparation of Borosilicate SSZ-44 10 Starting SiPy/ByO. = 50 j , Three mmol of a solution of Template A (5.33 grams, 0.562 mmol OHVg) were 1 9 mixed with 1.2 grams of 1.0 N NaOH and 5 4 grams of water Sodium borate 13 decahydrate (0.057 gram) was added to this solution and stirred until all ofthe solids had dissolved. Cabosil M-5 fumed silica (0 92 gram) was then added to the solution 14 and the resulting mixture was heated at 160°C and rotated at 43 φm for 14 days. A 15 settled product resulted, which was filtered, washed, dried and determined by XRD to 16 be SSZ-44. The product was found to have a SiO 2 B 2 O 3 mole ratio of 63. The X-ray 17 diffraction pattern representative o the as-made material is tabulated in Table V 18 below. 19 20 21 22 3 24 25 6 7 8 9 30 31 32 33 34 TABLE V 2 Theta d l OOxIJIn 2 Theta d lOOxI/Io 7.72 11.44 33.9 24.42 3.64 23.6 8.03 11.00 81.0 24.73 3.60 19.3 8.70 10.15 37.5 24.88 3.58 23. 1 12.61 7.01 10.7 25.13 3.54 37.0 15.33 5.78 20.7 25.58 3.48 37.7 15.96 5.55 25.2 25.70 2.36 19.7 17.02 5.20 6 8 26.24 3.39 20.5 17.91 4.95 16.4 27.02 3.30 25.2 19.16 4.63 100.0 27.66 3.22 10.9 19.71 4.50 6.1 27.96 3. 19 4.8 20.51 4.32 36.2 28.55 3. 12 15. 1 21.24 4.18 7.1 28.92 3.08 4.4 21.67 4.10 30.0 29.62 3.01 1 1.2 21.98 4.04 13.2 29.85 2.99 7.7 22.46 3.96 6.6 1.08 2.87 6.0 23.40 3.80 1 1.7 3 1.95 2.80 5.3 23.51 3.78 10.5 33.73 2.65 8.7 23.80 3.74 37.0 34.87 2.57 9.2 35.57 2.52 4.5 Exam pie 9 Preparation of A l-Silica SSZ-44 Three mmoles of a solution of Template A (5.24 g, 0.572 mmol OHVg) was mixed with 0.75 gram of 1.0 N KOH and 5.87 grams of water. Cabosil M-5 fumed silica (0.92 gram) was then added to the solution, followed by 0.005 gram of SSZ-44 seed crystals, and the resulting mixture was heated at 150°C for 1 days. The resulting settled product was filtered, washed and dried and determined by XRD to be SSZ-44 with a trace amount of layered material. Example 10 Calcination of SSZ-44 The material from Example 5 was calcined in the following manner. A thin bed of material was heated in a muffle furnace from room temperature to 120°C at a rate of 1°C per minute and held at 120°C for three hours. The temperature was then ramped up to 540°C at the same rate and held at th s temperature for 5 hours, after which it was increased to 594°C and held there for another 5 hours A 50/50 mixture of air and nitrogen was passed over the zeolite at a rate of 20 standard cubic feet per minute during heating Representative XRD data for the calcined product is given in Table VI below Example 1 1 Calcination of B-SSZ-44 The procedure descnbed in Example 10 was followed with the exception that the calcination was performed under a nitrogen atmosphere Example 12 N z Micropore Volume The product of Example 10 was subjected to a surface area and micropore volume analysis using N 2 as adsorbate and via the BET method The surface area of the zeolitic material was 430 M 2 /g and the micropore volume was 0 185 cc/g, thus exhibiting considerable void volume 1 Example 13 02 NH 4 Exchange 3 Ion exchange of calcined SSZ-44 material (prepared in Example 10) was 4 performed using NH4NO3 to convert the zeolite from its Na + form to the NI , form, 5 and, ultimately, the H * form. Typically, the same mass of NH NO3 as zeolite was 6 slurried in water at a ratio of 25-50: 1 water to zeolite. The exchange solution was 7 heated at 95°C for 2 hours and then filtered. This procedure can be repeated up to 8 three times. Following the final exchange, the zeolite was washed several times with 9 water and dried. This NH form of SSZ-44 can then be converted to the H * form by J O calcination (as described in Example 10) to 540°C. 1 , Example 14 NHi-Exchange of B-SSZ-44 12 The procedure described in Example 13 for ion exchange was followed with 13 the exception that NRjOAc was used in place ofthe NH4NO 3 . 14 Example 15 15 Constraint Index Determination 16 The hydrogen form ofthe zeolite of Example 7 (after treatment according to 17 Examples 10 and 13) was pelletized at 2-3 KPSI, crushed and meshed to 20-40, and 18 then > 0.50 gram was calcined at about 540°C in air for four hours and cooled in a 19 desiccator. 0.50 Gram was packed into a 3/8 inch stainless steel tube with alundum on 0 both sides ofthe zeolite bed. A Lindburg furnace was used to heat the reactor tube 1 Helium was introduced into the reactor tube at 10 cc/min. and at atmospheric pressure 2 The reactor was heated to about 315°C, and a 50/50 (w/w) feed of n-hexane and 3- 3 methylpentane was introduced into the reactor at a rate of 8 μl/min. Feed delivery was 4 made via a Brownlee pump. Direct sampling into a gas chromatograph began after 10 5 minutes of feed introduction. The Constraint Index value was calculated from the gas chromatographic data using methods known in the art, and was found to be 0.2. 7 At 315°C and 40 minutes on-stream, feed conversion was greater than 85%. 8 After 430 minutes, conversion was still greater than 60%. 9 It can be seen that SSZ-44 has very high cracking activity, indicative of 0 strongly acidic sites. In addition, the low fouling rate indicates that this catalyst has 1 good stability. The low CI. of 0.2 shows a preference for cracking the branched 2 alkane (3-methylpentane) over the linear n-hexane, which is behavior typical of large- 3 pore zeolites. 4 1 Example 16 2 Use of SSZ-44 To Convert Methanol 3 The hydrogen form of the zeolite of Example 6 (after treatment according to 4 Examples 10 and 13) was pelletized at 2-3 KPSI, then crushed and meshed to 20-40 5 0 50 Gram was loaded into a 3/8 inch stainless steel reactor tube with alundum on the 6 side ofthe zeolite bed where the feed was introduced The reactor was heated in a 7 Lindberg furnace to 1000°F for 3 hours in air, and then the temperature was reduced g to 400°C in a stream of nitrogen at 20 cc/min A 22 1% methanol feed (22.1 g 9 methanol/77.9 g water) was introduced into the reactor at a rate of 1.31 cc/hr. The 10 conversion at 10 minutes was 100%, and after 1 1 hours was still greater than 95% , j SSZ-44 makes very little light gas and produces considerable liquid product . „ under these conditions A large proportion of product is due to the formation of durenes, penta- and hexamethylbenzene (see Table C below) Formation of penta- and hexamethylbenzene is again indicative of a large pore zeolite, as the equilibrium 14 diameter ofthe latter is 7.1 Angstroms (Chang, C D., "Methanol to Hydrocarbons", 15 Marcel Dekker, 1983). 16 TABLE C 17 Product Wt % 18 Light gases 2 19 0 Xylenes 4 1 C aromatics 13 2 do aromatics 34 Pentamethylbenzene 24 4 Hexamethylbenzene 4 5 Other C10+ aromatics 19 6 Example 17 7 Pd Exchange 8 1.0 Gram of calcined and ammonium-exchanged SSZ-44 (made as described in 9 Example 2) was added to 10.0 grams of water and 1.0 gram of a 0.148 M NHiOH 0 solution to give a solution buffered at pH 9 5 Approximately 0 5 wt% Pd was loaded 1 onto the zeolite by ion exchange using a 0 05 M Pd(NH 3 ) 2NO 3 solution The mixture 2 was stirred at room temperature for 16 hours The solids were filtered and washed 3 with 1 iiter of water, dried, and calcined to about 482°C in air for three hours 4 Example 18 n ~Cj 6 Conversion - Hydrocracking The product of Example 17 was heated at 650°F in one atmosphere of hydrogen for two hours The product was then tested for its activity as a component in hydrocracking 0 5 Gram of catalyst was used for the test which consisted of running 1 mL/hour of n-hexadecane feed with 160 mL/minute of H 2 under the following conditions Temp 650°F WHSV 1 55 PSIG 1200 The results ofthe test are shown below nCjβ Conversion 97% Isomenzation selectivity 28% Cracking selectivity 72% nCiβ cracking conversion 70% C i n 1 3 C 6 i n 1 8 As shown above with the nCι 6 test feed, SSZ-44 can be used as a hydrocracking catalyst Example 19 Pt-B-SSZ-44 One gram of calcined and ammonium-exchanged B-SSZ-44 (prepared as descnbed in Examples 8, 1 1 and 14) was added to 10 0 grams of water and 1 0 gram of a 0 148 M NH4OH solution to give a solution buffered at about pH 9 5 Approximately 0 5 wt% Pt was loaded onto the zeolite by ion exchange using a 0 05 M Pt(NH3) 4 (NO 3 ) 2 solution The mixture was stirred at room temperature overnight The solids were filtered and washed with 1 liter of water, dried, and calcined to 288°C in air for 3 hours Example 20 Constraint Index and Activity of Pt-B-SSZ-44 The product from Example 19 was pelleted at 2-3 KPSI, crushed and meshed to 20-40 Then 0 50 gram was dried at 400°F in air for 4 hours and cooled in a desiccator 0 47 Gram was packed in the center of a 3/8 inch stainless steel tube with „ ,„„„,„ PCT/US96/18588 97/20769 -30- alundum on both sides of the zeolite bed A Lindburg furnace was used to heat the reactor tube. Helium was introduced into the reactor tube at 9 4 cc/min. and atmospheric pressure The reactor was taken to 800°F, and a 50/50 (w/w) feed of n- hexane and 3-methylpentane was introduced into the reactor at a rate of 10 μl min. Feed delivery was made via a piston pump Direct sampling onto a gas chromatograph began after introduction ofthe feed The constraint index value was calculated from gas chromatographic data using methods known in the art, and found to be 1 9 10 Minutes 40 Minutes Feed conversion, % 15 4 12 0 Prod Selectivities Cβ Isomerization 6 9 6 3 Cs. Cracking 13 1 9 2 Aromatization 6 9 4 9 Dehydrogenation 54 5 60 0

Claims: 01 WHAT IS CLAIMED IS: 02 03 1 A zeolite having an average pore size greater than about 6 Angstroms and 04 having the X-ray diffraction lines of Table I 05 06 2 A zeolite having a mole ratio greater than about 20 of an oxide of a first 07 tetravalent element to an oxide of a second trivalent or tetravalent element øg which is different from said first tetravalent element, and having the X-ray 09 diffraction lines of Table I 10 j j 3 A zeolite having a mole ratio greater than about 20 of an oxide selected from . the group consisting of silicon oxide, germanium oxide and mixtures thereof to an oxide selected from aluminum oxide, gallium oxide, iron oxide, boron oxide, 13 titanium oxide, indium oxide, vanadium oxide and mixtures thereof, and having 14 the X-ray diffraction lines of Table I 15 16 4. A zeolite according to Claim 3 wherein the oxides comprise silicon oxide and 17 aluminum oxide. 18 19 5 A zeolite according to Claim 3 wherein the oxides comprise silicon oxide and 20 boron oxide. 21 22 6 A zeolite according to Claim 3 wherein the oxides comprise silicon oxide and 23 titanium oxide. 24 5 7 A zeolite having a composition, as synthesized and in the anhydrous state, in 26 terms of mole ratios as follows 27 YO 2 /W.O b > 20 8 M7YO 2 < 0.05 9 Q/YO 2 0 01 - 0.10 30 where Q comprises a N,N-diethyl-cis-2,6-dimethyl piperidinium cation; M is an 1 alkali metal cation; W is selected from the group consisting of aluminum, 2 gallium, iron, boron, titanium, indium, vanadium and mixtures thereof; a = 1 or 3 2, b = 2 when a is 1 and b = 3 when a is 2, and Y is selected from the group 4 consisting of silicon, germanium and mixtures thereof 01 02 8 A zeolite according to Claim 7 wherein W is aluminum and Y is silicon. 03 04 9. A zeolite according to Claim 7 wherein W is boron and Y is silicon. 05 06 10 A zeolite according to Claim 7 wherein W is titanium and Y is silicon 07 ø 11 A zeolite having an average pore size greater than about 6 Angstroms and 0 having, after calcination, the X-ray diffraction lines of Table II. 10 j , 12 A zeolite having a mole ratio greater than about 20 of an oxide selected from 12 the group consisting of silicon oxide, germanium oxide and mixtures thereof to an oxide selected from the group consisting of aluminum oxide, gallium oxide, 13 iron oxide, boron oxide, titanium oxide, indium oxide, vanadium oxide and 14 mixtures thereof and having, after calcination, the X-ray diffraction lines of 15 Table II. 16 17 13 A zeolite according to Claim 1 1, wherein said zeolite is predominantly in the 18 hydrogen form. 19 20 14 A zeolite according to Claim 12, wherein said zeolite is predominantly in the 21 hydrogen form. 22 * " 15 A zeolite according to Claim 1 1 made substantially free of acidity by 24 neutralizing said zeolite with a basic metal. 25 26 16 A zeolite according to Claim 12 made substantially free of acidity by 27 neutralizing said zeolite with a basic metal 28 29 17 A method of preparing a crystalline material comprising one or a combination 30 of oxides selected from the group consisting of oxides of one or more first 31 tetravalent element(s) and one or more second trivalent or tetravalent 32 eiement(s) which is different from said first tetravalent element, said method 33 comprising contacting under crystallization conditions sources of said oxides 34 01 and a templating agent comprising a N,N-diethyl-cis-2,6-dimethylpiperidinium 02 cation. 03 04 18. The method according to Claim 17 wherein the first tetravalent element is 05 selected from the group consisting of silicon, germanium and combinations 06 thereof. 07 0g 19 The method according to Claim 17 wherein the second trivalent or tetravalent 09 element is selected from the group consisting of aluminum, gallium, iron, JO boron, titanium, indium, vanadium and combinations thereof. 1 1 20 The method according to Claim 1 8 wherein the second trivalent or tetravalent 12 element is selected from the group consisting of aluminum, boron, titanium and 13 combinations thereof 14 15 21 The method according to Claim 20 wherein the first tetravalent element is 16 silicon. 17 18 22 The method of Claim 17 wherein the crystalline material has the X-ray 19 diffraction lines of Table I 20 21 23 A process for converting hydrocarbons comprising contacting a hydrocarbonaceous feed at hydrocarbon converting conditions with a catalyst r -i comprising the zeolite of Claim 1 24 2 24 The process of Claim 23 wherein the catalyst comprises the zeolite of Claim 26 14 27 28 25 The process of Claim 23 wherein the catalyst comprises the zeolite of Claim 29 16. 30 3 1 26 A hydrocracking process comprising contacting a hydrocarbon feedstock under 32 hydrocracking conditions with a catalyst comprising the zeolite of Claim 1 33 34 01 27 A dewaxing process comprising contacting a hydrocarbon feedstock under 02 dewaxing conditions with a catalyst comprising the zeolite of Claim 1 03 04 28 A process for improving the viscosity index ofthe dewaxed product of waxy 5 hydrocarbon feeds comprising contacting the waxy hydrocarbon feed under 6 isomerization dewaxing conditions with a catalyst comprising the zeolite of 7 Claim 1. 8 29 A process for producing a C 2 o lube oil from a C 20+ olefin feed comprising j 0 isomerizing said olefin feed over a catalyst comprising the zeolite of Claim 1 , , and at least one Group VIII metal 12 30 A process for catalytically dewaxing a hydrocarbon oil feedstock boiling above 13 about 350°F and containing straight chain and slightly branched chain 14 hydrocarbons comprising contacting said hydrocarbon oil feedstock in the 15 presence of added hydrogen gas at a hydrogen pressure of about 15-3000 psi 16 with a catalyst comprising the zeolite of Claim 1 and at least one Group VIII 17 metal. 18 19 31 A process according to Claim 30 wherein said catalyst comprises a layered 0 catalyst comprising a first layer comprising the zeolite of Claim 1 and at least 1 one Group VIII metal, and a second layer comprising an aluminosilicate zeolite 2 which is more shape selective than the zeolite of said first layer. 23 4 32 A process for preparing a lubricating oil which comprises. 5 hydrocracking in a hydrocracking zone a hydrocarbonaceous feedstock 26 to obtain an effluent comprising a hydrocracked oil; and 7 catalytically dewaxing said effluent comprising hydrocracke i at a 28 temperature of at least about 400°F and at a pressure of from about psig to 29 about 3000 psig in the presence of added hydrogen gas with a catalyst 30 comprising the zeolite of Claim 1 and at least one Group VIII metal. 31 32 33. A process for isomerization dewaxing a raffinate comprising contacting said 33 raffinate in the presence of added hydrogen with a catalyst comprising the 34 zeolite of Claim 1 and at least one Group VIII metal 34 The process of Claim 33 wherein the raffinate is bright stock 35 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 200°C, under aromatic conversion conditions with the zeolite of Claim 1 36 The process of Claim 35 wherein the catalyst comprises the zeolite of Claim 16 37 The process of Claim 35 wherein the zeolite contains a Group VIII metal component 38 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 1 39 The process of Claim 38 wherein the catalyst additionally comprises a large pore crystalline cracking component 40 An isomerization process for isomerizing C to Ct hydrocarbons, comprising contacting a catalyst, comprising at least one Group VIII metal impregnated on the zeolite of Claim 1, with a feed having normal and slightly branched C 4 to C hydrocarbons under isomerizing conditions 1 The process of Claim 40 wherein the catalyst has been caicined in a steam air mixture at an elevated temperature after impregnation ofthe Group VIII metal 42 The process of Claim 41 wherein the Group VIII metal is platinum 43 A process for alkylating an aromatic hydrocarbon which comprises contacting under alkylation conditions at least a mole excess of an aromatic hydrocarbon WO 97/20769 -36- 1 with a C 2 to C 2 o olefin under at least partial liquid phase conditions and in the 2 presence of a catalyst comprising the zeolite of Claim 1. 3 4 44 The process of Claim 43 wherein the olefin is a C 2 to C 4 olefin. 5 6 45. The process of Claim 44 wherein the aromatic hydrocarbon and olefin are present in a molar ratio of about 4: 1 to about 20: 1 , respectively. 8 9 46 The process of Claim 44 wherein the aromatic hydrocarbon is selected from the J O group consisting of benzene, toluene, xylene, or mixtures thereof 11 47 A process for transalkylating an aromatic hydrocarbon which comprises 12 contacting under transalkylating conditions an aromatic hydrocarbon with a 13 polyalkyl aromatic hydrocarbon under at least partial liquid phase conditions 14 and in the presence ofthe zeolite of Claim 1 15 16 48 The process of Claim 47 wherein the aromatic hydrocarbon and the polyalkyl 17 aromatic hydrocarbon are present in a molar ratio of from about I 1 to about 18 25.1 , respectively. 19 20 49 The process of Claim 47 wherein the aromatic hydrocarbon is a member 1 selected from the group consisting of benzene, toluene, xylene, or mixtures 22 thereof. 23 24 50 The process of Claim 47 wherein the polyalkyl aromatic hydrocarbon is a 5 dialkylbenzene. 26 2 51 A process to convert paraffins to aromatics which comprises contacting 28 paraffins with a catalyst comprising the zeolite of Claim 1 and gallium, zinc, or 29 a compound of gallium or zinc 30 31 52 A process for converting lower alcohols and other oxygenated hydrocarbons 32 comprising contacting said lower alcohol or other oxygenated hydrocarbon 33 with a catalyst comprising the zeolite of Claim 1 under conditions to produce 34 liquid products. 01 02 53 A process for isomerizing olefins comprising contacting said olefin with a 03 catalyst comprising the zeolite of Claim 1 under conditions which cause 04 isomerization ofthe olefin 05 06 54 A process for isomerizing an isomerization feed comprising an aromatic Cg 07 stream of xylene isomers or mixtures of xylene isomers and ethylbenzene, ø wherein a more nearly equilibrium ratio of ortho-, meta and para-xylenes is 09 obtained, said process comprising contacting said feed under isomerization j 0 conditions with a catalyst comprising the zeolite of Claim 1 12 55 A process for oligomerizing olefins comprising contacting an olefin feed under oligomerization conditions with a catalyst comprising the zeolite of Claim 1 13 14 56 The process of Claim 26, 27, 28, 29, 30, 32, 33, 38, 40, 43, 47, 51, 52, 53, 54 15 or 55 wherein the zeolite is predominantly in the hydrogen form 16 17 57 In a process for the reduction of oxides of nitrogen contained in a gas stream in 18 the presence of oxygen wherein said process comprises contacting the gas 19 stream with a zeolite, the improvement comprising using as the zeolite a zeolite 20 having a mole ratio of an oxide of a first tetravalent element to an oxide of a 21 second trivalent or tetravalent element which is different from said first 22 tetravalent element, said mole ratio being greater than about 20 and having the 23 X-ray diffraction lines of Table I 24 2 58 The process of Claim 57 wherein said zeolite contains a metal or metal ions 26 capable of catalyzing the reduction ofthe oxides of nitrogen 27 8 59 The process of Claim 58 wherein the metal is copper, cobalt or mixtures 29 thereof. 30 31 60 The process of Claim 58 wherein the gas stream is the exhaust stream of an 32 internal combustion engine 33 34

Inventors: YUMI NAKAGAWA, YUMI, NAKAGAWA
Applicants: CHEVRON USA INC, CHEVRON U.S.A. INC.
Application year: 1996
Main classification: C01B39
IPC codes: B01J29, C01B37, C01B39, C07B61, C07C2, C07C5, C10M101, C10N20