HYDROCARBON CONVERSION CATALYSTS, METHODS OF MAKING THEM AND THEIR USES IN HYDROCARBON CONVERSION

Abstract: Hydrocarbon conversion catalyst comprising an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component, and a support component compris­ ing at least one porous refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component.

Description: HYDROCARBON CONVERSION CATALYSTS, . < METHODS OF MAKiNG THEM AND THEIR USES IN HYDRUCARBON CONVERSION BACKGROUND OF THE INVENTION This invention relates to improved catalytic compositions having utility in hydrocarbon conversion processes. In a specific aspect, the invention relates to improved catalytic compositions having utility in hydrogen treating of hydrocarbon feed materials. Catalytic compositions containing a catalytically active metallic component deposed on a non-zeolitic, refractory inorganic oxide- support are well known as are numerous uses therefor. Familiar examples include petroleum and synthetic crude oil hydrotreating and hydrocracking catalysts comprising a Group VIB andor VIII metal such as cobalt, nickel, molybdenum and/or tungsten deposed on a non-zeolitic, refractory inorganic oxide such as alumina, silica, magnesia, etc. ad olefin polymerization catalysts comprising a Group VIB metal deposed on silica or silica-alumina supports. It also is known that the activity or performance of catalysts of the type described hereinabove for reactions such as hydrocracking, disproportionation and oligomerization can be improved or modified by inclusion in the catalyst of a crystalline molecular sieve zeolite component. Thus U.S. 3,649,523 (Bertolacini et al.) discloses a hydrocarbon conversion process, and particularly hydrocracking and disproportionation of petroleum hydrocarbon feed materials, carried out in the presence of improved catalysts comprising a metallic component having hydrogenating activity deposed on a support component comprising a large pore crystalline aluminosilicate and a porous support material such as alumina, silica or aluminum phosphate. U.S.. 3,894,930 and U.S. 4,054,539 (both Hensley) disclose hydrocracking in the presence of improved catalysts comprising a metallic hydrogenating component and a support component comprising ultrastable large pore crystalline aluminosilicate and silica-alumina. U.S. 3,876,522 (Campbell et al.) discloses preparation of lube oils by a process that includes a hydrocracking step in which there are employed catalysts containing a composite of a crystalline aluminosilicate zeolite component and a porous refractory oxide component such as alumina or silica, such composite containing deposited or exchanged catalytic metals U.S. 4,029,601 (Wiese) discloses oligomerization of alkenes using a cobalt oxide-active carbon composite supported on a refractory oxide such as silica or alumina and/or crystalline aluminosilicate zeolites. Other processes in which catalysts comprising catalytically active metals and a support component comprising a porous oxide and a crystalline molecular sieve zeolite are useful include isomerization of alkylaromatics and alkylation of aromatics and paraffins. Zt also is known that the performance of various catalysts. containing catalytically active metals deposed on a non-zeolitic, refractory inorganic oxide support component can be improved or modified by inclusion of phosphorus in the catalytically active metallic component or through the use of phosphorus compounds in catalyst preparation. For example, U.S. 3,287,280 (Colgan et al.) discloses that the use of phosphoric acid solutions of nickel and/or molybdenum salts to impregnate non-zeolitic supports such as alumina or silica leads to improved dispersion of catalytically active metals on the support surface and improved results in hydrodesulfurization of petroleum hydrocarbon feeds. The patentee also discloses that phosphoric acid residues remaining in the catalyst impart thermal stability thereto.. U.S. 3,840,472 (Colgan) contains a similar disclosure with respect to the use of phosphoric acid impregnating solutions of active metal salts. U.S. 4,165,274 (Kwant) discloses a two-step process for hydrotreating and hydrocracking tar sands oils wherein hydrotreating takes place in a first stage in the presence of an alumina-supported, fluorine and phosphorus-containing nickel-molybdenum catalyst, after which hydrocracking is conducted in the presence of a. catalyst-containing nickel and tungsten supported on a low-sodium, Y-type molecular sieve support component. U.S. 3,985,676 (Rekers et al.) discloses catalysts for polymerization of olefines prepared by deposition of various organophosphorus compounds of chromium onto high surface area non-zeolitic supports such as. silica or silica-alumina followed by thermal activation of the result. Notwithstanding similarities in the basic catalytic composition--catalytically active metal component deposed on non-zeolitic refractory inorganic oxide support component--into which phosphorus or crystalline molecular sieve zeolite components have been incorporated according to the above-described proposals, the reported effects of the zeolite and phosphorus components are, in many respects, sufficiently unrelated as to mitigate against attempting to combine the effects of the components into a single catalyst. For example, the improved hydrocracking activity of the above-described zeolitecontaining catalysts typically would not be desired in a hydrodesulfurization or hydrodenitrogenation catalyst because in typical hydrotreating processes employing such catalysts, it is preferred to limit cracking. Similarly, the improved hydrocesulfuri- zation activity of phosphorus-promoted catalysts such as those of Colgan et al. would be of little consequence within the context of a cracking, alkylation, isomerization or disproportionation process. On the other hand, we have previously found that a phosphorus component incorporated into the hydrogenating component of certain hydrotreating catalyst exerts a promotional effect with respect to denitrogenation of high nitrogen feeds while crystalline molecular sieve zeolite components incorporated into catalysts containing similar active metals but free of phosphorus exerts a promotional effect with respect to denitrogenation and hydrocracking reactions tt also is known from Rabo, Zeolite Chemistry and Catalysis, ACS Monograph 171, American Chemical Society, pages 294-297 (1976), that many crystalline molecular sieve zeolites possess only limited stability with respect to strong acids such as the phosphoric acid used according to Colgan et al. Accordingly, it can be speculated that attempts to combine the promotional effects of phosphoric acid and crystalline molecular sieve zeolites have been limited by concern over destruction of the zeolite component. U.S. 3,617,528 (Hilfman), which is directed to preparation of supported nickel-containing catalysts by coextrusion of a phosphoric acid solution of nickel or nickel and Group VIB metal compounds and an alumina-containing carrier, suggests the use of carriers containing silica and alumina that are amorphous or zeolitic in nature. Column 2 lines 39-43. Crystalline aluminosilicate zeolites specifically disclosed by Hilfman are mordenite, faujasite and Types A and U molecular sieves. Column 3 lines 42-46. Hilfman does not address the effect of the acid on zeolite integrity or crystallinity, nor is there any disclosure or suggestion as to whether any zeolite- employed in the disclosed preparations would remain intact in the final catalyst. In fact, none of the disclosed crystalline aluminosilicate zeolites, or any other for that matter, is employed in the patentee's examples. Further, U.S. 3,706,693 (Mickelson et al. '693) and U.S. 3,725,243 (Hass et al.) teach that exposure of zeolites to strong acids such as phosphoric acid destroys zeolite crystallinity and integrity. In fact, both Mickelson et al. '693 and Hasps et al. are directed specifically to catalyst preparations in which impregnation of crystalline aluminosilicate-containing supports with phosphoric acid solutions of salts of hydrogenating metals results in destruction of zeolite crystallinity. Further, three of the four crystalline aluminosilicate zeolites specifically disclosed by Hilfman (faujasite, mordenite and Type A molecular sieve) are included among the crystalline- aluminosilicate zeolites that are preferred for use in Mickelson et al.'s and Hasps et al.'s zeolite-destructive preparations. The aforesaid Rabo publication teaches that among Zeolite A, faujasite and mordenite, only the latter exhibits appreciable acid stability. u.S. 3,905,914 (Jurewicz et al.) is directed to preparation of oxidation catalysts by mixing a vanadium compound, zirconium salt and hydrogen halide, and then adding phosphoric acid or a compound hydrolyzable to phosphoric acid. The result is refluxed to form a gel which then is dried, or "used to impregnate a suitable carrier, such as alumina, alundum, silica, silicon carbide, silica-alumina, zirconia, zirconium phosphate and/or a zeolite." Column 2 lines 47-51. Jurewicz et al. does not identify any zeolites nor do the patentees examples illustrate preparation of a supported catalyst. Also, no consideration is given to acid stability of zeolites and there is no indication whether any zeolite used in the disclosed catalyst preparation would remain intact. Similar to the Mickelson et al. '693 and Hass et al. patents discussed hereinabove, U.S. 3,749,663, 3,749,664 and 3,755,150 (all Mickelson) are directed to impregnation of support materials with phosphoric acid solutions of salts of catalytically active metals Although none of these patents discloses impregnation of support materials containing a zeolite component, each patent expressly cautions against exposure of supports containing aluminum ions to phosphoric acid at relatively low pH stating that reaction of the acid and aluminum degrades the support, fouls the impregnation solution and results in formation of undesirable chemical forms in the finished catalyst. (See Mickelson '663 at Column 8 lines 60-69, Mickelson '664 at Column 8 lines 6-15, Mickelson '150 at Column 9 lines 12-21.) U,S.. 3,836,561 (Young) also deals with acid treatment of crystalline aluminosilicate zeolites. According to Young, alumina-containing compositions, including those containing crystalline aluminosilicate zeolites, are reacted with aqueous acids including hydrochloric, sulfuric, nitric, phosphoric and various organic acids, at a pH below 5 in the presence of an ionizable salt that is soluble in the aqueous phase, and then the result is washed, dried and calcined. The result of such treatment is removal of aluminum from the alumina-containing composition, replacement thereof with metallic cations if the ionizable salt is one containing cations that can be exchanged into the zeolite, increased porosity and decreased bulk volume of the catalyst. The resulting compositions are said to have utility as absorbents, ion exchange resins, catalysts and catalyst supports. Acid-stable zeolites and the effects of acid treatment on zeolite crystallinity are discussed at Column 2 lines 61-68. Of course, Young's acid treatment differs from the use of phosphoric acid according to the patents discussed hereinabove in that Young's purpose is to remove aluminum from the composition rather than to incorporate phosphorus into it. It also differs from the patents discussed hereinabove in that the disclosed compositions lack a catalytically-active metallic component deposed on the alumina-containing carrier. Other patents and publications that may be of interest to the present invention in disclosing treatment of crystalline molecular sieve zeolites or compositions containing the same with phosphoric acid and other phosphorus compounds to incorporate phosphorus into the zeolite are U.S. 3,962,364 (Young) and U.S. 4,274,982, 4,276,437 and 4,276,438 (all Chu) According to these patents, suitable phosphorus compounds include halides, oxyhalides, oxyacids, and organophosphorus compounds such as phosphines, phosphites and phosphates. Incorporation of phosphorus according to these patents is reported to improve para-selectivity in alkylation reactions. Chu '982 further discloses treatment of the phosphoruscontaining zeolites with magnesium compounds. Chu '437 discloses impregnation of the phosphorus treated compositions with solutions of gallium, iridium or thallium compounds. Chu '438 contains a similar disclosure with respect to impregnation of compounds of silver, gold and copper. Both patents disclose use of acid solutions of the metals as impregnating solutions, with hydrochloric, sulfuric and nitric as well as various organic acids being disclosed. None of these patents discloses or suggests the use of phosphoric acid impregnating solutions nor is there any suggest ion of a catalyst containing an active metallic component which contains phosphorus, Rather, the respective patentees' phosphorus is incorporated into the zeolite. British 1,555,928 (Kouwenhaven et al.) discloses crystalline silicates of specified formula having utility in a wide range of hydrocarbon conversions. Impregnation of the silicates with catalytic metals is disclosed as is promotion or modification with halogens, magnesium, phosphorus, boron, arsenic or antimony, (Page 6 lines 33-54); with incorporation of phosphorus into the silicate to improve alkylation selectivity, as in the above-described Chu patents, being specifically disclosed It also is known that phosphine or other organophosphorus complexes of various metal salts can be employed in preparation of various supported catalyst compositions. For example, U.S. 3,703,561 (Kubicek et al.) discloses catalysts for olefin disproportionation comprising a reaction product of (1) an organoaluminum halide, aluminum halide or combination thereof with each other or with another organometallic halide and (2) a mixture of a salt of copper, silver or gold with a complexing agent which may be an organophosphine. Reaction of components (1) and (2) is conducted in the presence of a solvent for the reactants, in the substantial absence of air and at temperatures low enough to avoid decomposition of the reactants. It also is disclosed to provide the catalysts in supported form by impregnating a support such as a non-zeolitic, refractory inorganic oxide or a zeolite with the reaction product, or by impregnation with one of the reactants followed by addition of the other. Kubicek et al. also states that if such supported catalysts are to be activated by calcination the calcination should take place prior to impregnation with the active species, i.e., the reaction product of components (1) and (2). It is unclear whether residues of any organophosphine compound used in preparation of the catalysts of Kubicek et al. would remain in association with the active metallic species. In any event, the catalyst preparation according to this patent is conducted under conditions designed to avoid conversion of any such organophosphine residues to an oxygenated phosphorus component such as that required according to the present invention. U.S. 3,721,718 (Hughes et al.) and U.S. 4,010,217 (Zuech) contain disclosures similar to that of Kubicek et al. with respect to use of organophosphorus complexes of various metal salts in preparation of olefin disproportination catalysts. Like Kubicek et al., both Hughes et al. and Zuech contemplate supported catalysts; however, both patentees also state that if activation by calcination is desired, it should be accomplished by calcination of support prior to incorporation of active metals. Another patent disclosing the use of metal complexes in catalyst preparation is U.S. 3,849,457 (Haag et al.) which is directed to preparation of carboxylic acids by hydrogenolysis of esters. T'ne catalysts of Haag et al. comprise a hydrogenating metal component and a solid acid component such as a zeolite which components may be employed as a loose physical admixture or by combining the two components into a single particle. Various methods for combining the two components into a single particle are disclosed at Column 6 line 64-Column 7 line 44. One of these involves mixing a solution of a metal pi-complex with the acid solid and then decomposing the complex to form elemental metal and depositing the elemental metal onto the acid solid. A specific metal complex employed in this preparative scheme is tetra(triphenylphosphine)palladium(II) dibromide. Another preparative method useful with respect to zeolitic acid solid components involves incorporation of the hydrogenation component by conventional methods such as ion exchange or impregnation. None of the disclosed methods would result in association of an oxygenated phosphorus component with the metallic component of the patentees' catalyst. U.S., 4,070,403 (Homeier) discloses a hydroformylation catalyst comprising a cobalt compound and a. zeolite-alumina hydrosol dispersion. The cobalt compound is chemically bonded to the aluminazeolite dispersion by a vapor-phase impregnation technique. Suitable cobalt components, of the disclosed catalysts include various salts such as halides t nitrate and various carboxylates as well as organophosphine complexes. Homer does not disclose or suggest the presence of an oxygenated phosphorus component in the final catalyst, nor does the patentee attribute any promotional effect to phosphorus It can be appreciated from the foregoing that efforts to include both a crystalline molecular sieve zeolite component and a phosphorus component in catalysts comprising an active metal component deposed on a non-zeolitic refractory inorganic oxide component in such a manner that the promotional effects of both the phosphorus and the zeolite are retained have been largely unsuccessful. In those instances in which an attempt has been made to incorporate a promoting phosphorus component through the use of phosphoric acid impregnating solutions of compounds of active metals, such use of phosphoric acid in conjunction with a crystalline aluminosilicate zeolite-containing composition often results in destruction of the crystalline aluminosilicate zeolite component. Other proposals such as those involving use of organophosphorus complexes of various metal salts to aid impregnation or deposition of active metals into or onto support result in only incidental, if any, incorporation of phosphorus into the final catalyst, and phosphorus so incorporated appears lacking- in promotional effect It would be desirable to provide an improved catalytic composition in which both phosphorus and crystalline molecular sieve zeolite components are present in a form capable of exerting a promotional effect. It is an object of this invention to provide an improved catalytic composition. A further object of the invention is to provide for the use of such catalytic compositions in hydrocarbon conversion processes. A still further object is to provide for the preparation of catalysts in which improved performance is attained through incorporation of crystalline molecular sieve zeolite and phosphorus components. Other objects of the invention will be apparent to persons skilled in the art from the following description and the appended claims. We have now found that the objects of this invention can be attained by incorporation of an oxygenated phosphorus component into the catalytically active metallic component of a catalytic composition and incorporation of selected crystalline molecular sieve zeolite components into the support component of the composition. Advantageously, the crystalline molecular sieve zeolite components of the invented catalysts are derived from acid-tolerant crystalline molecular sieve zeolites, and accordingly, phosphorus component can be incorporated without substantial destruction of zeolite integrity or crystallinity. Further, the phosphorus component is incorporated into the metallic component in a form capable of exerting a promotional effect. Thus, as demonstrated in the examples appearing hereinbelow, the catalysts of the invention, wherein an oxygenated phosphorus component is incorporated into a catalytically active metallic component which is deposed on or associated with a support component comprising at least one crystalline molecular sieve zeolite component and a non-zeolitic, refractory inorganic oxide matrix component, are superior to catalyst compositions that are identical but for the inclusion of a phosphor-us component, or but for inclusion of the zeolite component, in a variety of catalytic processes. Aecordingly, the overall effect of the phosphorus and zeolite components on performance of the basic catalytically active composition comprising a metallic component and a non-zeolitic, refractory inorganic oxide component is- greater than the effect of either component alone in a variety of reactions. In addition to the patents and publications discussed hereinabove, U.S. 4,228,036 (Swift et al.) and UtS, 4,277,373 (Sawyer et al.) may be of interest to the present invention in disclosing catalytic compositions containing phosphorus and zeolite components. Specifically, Swift et al. discloses an improved catalytic cracking catalyst comprising an alumina-aluminum phosphate-silica matrix composited with a zeolite component having cracking activity, such as a rare earth-exchanged Y-type crystalline aluminosilicate zeolite. Swift et al. does not disclose inclusion of an active metallic component into such catalysts. Further, in contrast to the catalysts of the present invention, wherein an oxygenated phosphorus component is included in an active metallic component, the phos phorus component of Swift et al.'s catalysts is included in a refractory oxide material. Sawyer et al. discloses hydroprocessing catalysts comprising a Group VIB and/or VIII metal component composited with an ultrastable Y-type crystalline aluminosilicate zeolite and an alumina-aluminum fluorophosphate component. The catalyst also may contain an alumina gel-containing matrix. Although an essential component of Sawyer et al.'s catalyst is the aluminum fluorophosphate component of the support, it also is to be noted. that patentee. discloses use of phosphomolybdic acid to impregnate a support containing a Y-type crystalline aluminosilicate and alumina-aluminum fluorophosphate in Example 1 (see Column 5 lines 21-25). According to the example, however, it appears that there was no incorporation of a phosphorus component into the active metal component of the catalyst because the table at Column 5 lines 42-52 fails to report phosphorus content other than that contained in the aluminum fluorophosphate component of the support. Table 2 of Sawyer et al. also reports on a comparative catalyst C containing specified levels of alumina, Y-type zeolite, nickel oxide, molybdenum oxide, and phosphorus pentoxide. For catalyst C to have been a fair comparator for the catalysts of Sawyer et al.'s invention, the phosphorus pentoxide component must have been present in a manner similar to the fluorophosphate component of the patentees' catalysts, i.e., as part of the support. As such, Sawyer et al. fails to disclose or suggest a catalyst containing phosphorus as an essential part of the active metal component. DESCRIPTION OF THE INVENTION Briefly, the catalyst composition of this invention comprises (1) an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component; and (2) a support component comprising at least one non-zeolitic, refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component. According to a further aspect of the invention, such catalytic compositions are prepared by a method comprising (1) impregnating a support component comprising at least one non-zeolitic, refractory inorganic oxide matrix component and at least one acid-tolerant, crystalline molecular sieve zeolite component with percursors to an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component under conditions effective to retain substantial zeolite crystallinity; and (2) calcining the result to convert active metallic component precursors to active form. According to a still further aspect of the invention, the abovedescribed catalytic compositions are employed in hydrocarbon conversion processes in which a hydrocarbon-containing chargestock is contacted with the catalytic composition under hydrocarbon conversion conditions In greater detail, the invented catalytic composition comprises an active metallic component and a support component. Relative proportions of these are not critical so long as the active metallic component is present in at least a catalytically effective amount. Optimum proportions for a given catalyst will vary depending on intended use. Usefully, the active metallic component constitutes 5 to 50 wt and the support constitutes 50 to 95 wt%, such weight percentages being based upon total weight of the catalytic composition. The active metallic component of the invented catalyst comprises at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component. Suitable metals having hydrocarbon conversion activity include any of the metals typically employed to catalyze hydrocarbon conversion reactions such as those of Groups IB, II t IIIB-VIIB and VIII. These can be present in the catalyst in elemental form, as oxides, as sulfides, or in other active forms. Combinations also are contemplated. The Group VIB metals exhibit a high degree of susceptibility to promotion by oxygenated phosphorus component. Accordingly, preferred compositions are those in which the active metallic component comprises at least one Group VIB metal. For a given catalyst, the preferred metal or combination of metals of the active metallic component will vary depending on end use. For example, in hydrogen processing of hydrocarbon feed materials such as petroleum or synthetic crude oils, coal or biomass liquids, or fractions thereof, preferred metals are those of Groups VIB and VIII such as chromium, molybdenum, tungsten, nickel, cobalt, iron, platinum, rhodium, palladium, iridium and combinations thereof. Oxides and sulfides of these are most preferred from the standpoint of catalytic performance. In processes for denitrogenation hydrotreating or denitrogenation hydrocracking, combinations of nickel or cobalt with molybdenum and chromium give particularly good results. Particularly good results in hydrocracking processes are attained using catalysts containing combinations of cobalt and molybdenum, nickel and molybdenum, or nickel and tungsten as the metals of the active metallic component. In mild hydrocracking processes such as catalytic. dewaxing and catalytic cracker feed hydrocracking processes, preferred metals of the metallic component are combinations of nickel and molybdenum. In addition to the above-described catalytically active metal component, the active metallic component of the invented composition contains at least one oxygenated phosphorus component which may be present in a variety of forms such as one or more simple oxides, phosphate anions, complex species in which phosphorus is linked through oxygen to one or more metal or metals of the active metallic component or compounds of such metal or metals, or combinations of these. The specific form of the oxygenated phosphorus component is not presently known; accordingly, for purposes hereof, phosphorus contents are calculated and expressed in terms of P2O5. Content of the metal and phosphorus components of the active metallic component is not critical although phosphorus component preferably is present in at least an amount effective to promote hydrocarbon conversion activity of the metal or metals of the metallic component. In general, the metal or metals of the metallic component, calculated as oxide of the metal or metals in a common oxidation state, e.g., Cr203, MoO3, W03, NiO, CoO, make up 3 to 45 wt.t of the total catalyst weight while phosphorus component, expressed as P205, makes up 0.1 to 20 wt.% of the total catalyst. Within these broad ranges, preferred levels of metal and phosphorus component will vary depending on end use. For example, catalysts useful in hydrogen processing of petroleum or synthetic crude oils, coal or biomass liquids, or fractions thereof preferably contain 5 to 35 wt.% Group VIB and/or VIII metal, expressed as common metal oxide, and 0.5 to 15 wt.% oxygenated phosphorus component, expressed as P2O5. Of course, higher and lower levels of metal and/or phosphorus component can be present; however, below 5 wt.% metal oxide, hydrogenation activity can suffer while above 35 wt.%, improvements in activity typically do not compensate for the cost of the additional metal. Similarly, below 0.5 wt.% phosphorus component, calculated as P205, promotional effect may be insignificant while above 15 wt.%, the phosphorus component may adversely affect hydrogenation activity or performance. For high nitrogen feedstocks, the hydrogenating metal preferably makes up 10 to 40 wt.% of overall catalyst while phosphorus content as P205 makes up 0.5 to 15% of overall catalyst weight. For mild hydrocracking, hydrogenating metal preferably makes up 5 to 30 wt.% of overall catalyst weight while phosphorus content as P205 makes up 0.1 to 10 wot.% of overall catalyst weight. The support component of the invented catalytic composition comprises a non-zeolitic, refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component. Suitable non-zeolitic, refractory inorganic oxide matrix components are well known to persons skilled in the art and include alumina, silica, silica-alumina, alumina-silica, magnesia, zirconia, titania, etc., and combinations thereof. The matrix component also can contain adjuvants such as phosphorus oxides, boron oxides, fluorine and/or chlorine. Matrix components that are preferred are those comprising alumina, owing to the availability and strength thereof. More preferably, the matrix component is alumina, or a combination of alumina and silica. The support component of the invented catalytic composition also comprises at least one crystalline molecular sieve zeolite component. This component of the support component is derived from at least one acid-tolerant crystalline molecular sieve zeolite. For purposes hereof, an acid-tolerant crystalline molecular sieve zeolite is defined as one that retains substantial crystallinity on exposure to phosphoric acid at pH down to about 3 to 4 and contains sufficiently low levels of cations capable of reacting with aqueous phosphoric acid to form insoluble metal phosphates capable of plugging the zeolite's pores as to avoid substantial plugging. Both naturally occurring and synthetic zeolites are contemplated. As with the metals of the metallic component of the invented catalysts, the specific zeolite component to be included in a given catalyst will vary depending on intended use of the catalytic composition. Examples of acid-tolerant, crystalline molecular sieve zeolites include faujasite-type crystalline aluminosilicate zeolites selected from the ultrastable Y-type crystalline aluminosilicate zeolites in acid and ammonium forms, AMS-type crystalline borosilicate zeolites, ZSM-type crystalline aluminosilicate zeolites and mordenite-type crystalline aluminosilicate zeolites. The ultrastable crystalline aluminosilicate zeolites typically are faujasite-type zeolites that exhibit improved stability at elevated temperatures, such stability being imparted by exchanging original alkali metal cations with ammonium salt, calcining to convert the zeolite to hydrogen form, steaming or calcining again, exchanging with ammonium salt once again and finally calcining. Specific examples of ultrastable Y-type crystalline aluminosilicate zeolites include zeolite Z-l4US, which is described in detail in U.S. 3,293,192 (Maher et al.) and U.S. 3,449,070 (McDaniel et al.), both of which are incorporated herein by reference. Y-type crystalline aluminosilicate zeolites in hydrogen or ammonium form also exhibit sufficient acid-tolerance as to be suitable for purposes of the present invention. When used in preparation of catalysts, Y-type zeolites in ammonium form are converted to acid form. Crystalline borosilicate zeolites of the AMStype are described in detail in commonly assigned U.S. 4,269,813 (Klotz), which is incorporated herein by reference. A specific example of this material is crystalline borosilicate zeolite AMS-lB which corresponds to the formula: 0.9 + 0.2 M2/n0:B203:YSi02:ZH2Or wherein M is at least one cation having a valence of n, Y ranges from 4 to about 600 and Z ranges from 0 to 160. , AMS-.lB provides an X-ray pattern that comprises the following X-ray diffraction lines and assigned strengths: : d nm (A) Assigned Strength 1.12 + 0.02 11.2 + 0.2 W-VS 1.00 + 0.02 10.0 + 0.2 W-MS 0.597 1 0.007 5.97 + 0.07 W-M 0.382 + 0.005 3.82 T 0.05 VS 0.370 t 0005 3.70 t 0.05 MS 0.362 W 0.005 3.62 F 0.05 M MS 0.297 t 0.002 2.97 + 0.02 W-M 0.199 + 0.002 1.99 + 0.02 Crystalline aluminosilicate zeolites of the ZSM-type are well known and typically contain silica and alumina in a molar ratio of at least 12:1 (SiO2: :A12G3) and have average pore diameters of at least 0.Snm (5 ). Specific examples of crystalline aluminosilicate zeolites of the ZSM-type include crystalline aluminosilicate zeolite ZSM-5, which is described in detail in U.S. 3,702,886; crystalline aluminosilicate ZSM-11, which is described in detail in U.S. 3,709,979; crystalline aluminosilicate zeolite ZSM-12, which is described in detail in U.S. 3,832,449; crystalline aluminosilicate zeolite ZSM 35, which is described in detail in U.S. 4,016,245; and crystalline aluminosilicate zeolite ZSM-38, which is described in detail in U.S. 4,046,859. All of the aforesaid patents are incorporated herein by reference. Mordenite-type crystalline aluminosilicate zeolites also can be present in the catalytic compo sition of the- present invention. Suitable mordenite type crystalline aluminosilicate zeolites are dis closed in U.S. 3,247,098 (Kimberline), U.S. 3,281,483 (Benesi et al.) and U.S. 3,299,153 (Adams et al.), each of which is incorporated herein by reference. Synthetic mordenite-structure crystalline aluminosil icate zeolites1 such as those designated Zeolon and available from the Norton Company of Worcester, Massachusetts, also are contemplated according to the invention. Synthetic crystalline molecular sieve zeolites often are synthesized in alkali metal form, i.e., having alkali metal cations associated with framework species For purposes of the present invention, the original form as well as various exchanged forms such as the hydrogen (acid), ammonium and metalexchanged forms are suitable. Crystalline molecular sieve zeolites can be converted to acid form by exchange with acids or by indirect means which typically involve contacting with ammonium or amine salts to form ammonium-exchanged intermediate species which can be calcined to acid form. Metal-exchanged zeolites are well known as are methods for preparation thereof. Typically, zeolite is contacted with a solution or solutions containing metal cations capable of associating with framework metallic species. As noted hereinabove, crystalline molecular sieve zeolite components present in the catalysts of the present invention contain only insubstantial levels of metals capable of reacting with aqueous phosphoric acid to form insoluble metal phosphates capable of plugging the pores of the support component. Accordingly, preferred metal-exchangeÅa crystalline molecular sieve zeolites are those in which the exchanged metals are nickel, cobalt, iron or a Group VIII noble metal. In catalysts intended for use in hydrogen processing of petroleum or synthetic crude oils, coal or biomass liquids, or fractions thereof, preferred crystalline molecular sieve zeolite components of the invented catalysts are those in acid or polyvalent metal ion-exchanged form, and especially the former. Content of non-zeolitic, porous refractory inorganic acid matrix component and crystalline molecular sieve zeolite component in the support component of the invented composition are not critical. Broadly, the matrix component constitutes 5 to-95 wt of the support, and likewise, the zeolite component can constitute 5 to 95 wt of the support Preferably, the content of the non-zeolitic matrix component is at least 10 wt% in order to ensure that the support component will exhibit sufficient strength and physical integrity to allow shaping of the component or final catalyst into a form suitable for intended use Of course, even at less than 10 wt mat-rix component, suitable catalytic performance can be attained in applications amenable to use of catalyst in finely divided form. In terms of overall catalyst weight of the invented catalytic Pomposition, preferred matrix 'content ranges from 10 to 90 wt%- and preferred zeolite content ranges from 5 to 90 wt, Within these ranges, precise levels of matrix and zeolite components that are more preferred for a given catalyst will vary depending on intended use. For use in mild hydrocracking, the matrix component content preferably ranges from 40 to 95 wt.t of the support while zeolite content ranges from 5 to 60 wt.% of the support component. The support component of the invented catalytic composition can be prepared by any suitable method. A preferred method comprises blending acid-tolerant zeolitic component, preferably in finely divided form, into a sol, hydrosol or hydrogel of at least one inorganic oxide and adding a gelling medium such as ammonium hydroxide with stirring to produce a gel. It also is contemplated to add the zeolite component to a slurry of the matrix component. In either case, the result can be dried, shaped if desired, and then calcined to form the support component Suitable drying temperatures range from 27 to 1770C (80 to 350oF) and suitable drying times range from seconds to several hours. Calcination preferably is conducted at a temperature of 427 to 6490C (00 to 1,2000F) for 1/2 to 16 hours. Shaping of the support component can be conducted if desired, preferably after drying or calcining. Another suitable method for preparing the support component of the invented composition comprises physically mixing particles of the matrix and zeolite components, each preferably in finely divided form, followed by thorough blending of the mixture. The invented catalytic composition is prepared by a method comprising (1) impregnating the abovedescribed support component with precursors to the active metallic component under conditions effective to retain substantial zeolite crystallinity; and (2) calcining the result. Impregnation of support component with precursors to the active metallic component can be conducted in a single step or in a series of separate steps which may be separated by drying and/or calcination steps, provided that impregnation with at least one metal precursor takes place prior to or simultaneously with impregnation with. phosphorus component precursor. If the active metallic component contains more than one metal, precursors can be impregnated simultaneously, in sequence or by various combinations of simultaneous and sequential impregnations. Phosphorus component precursor or precursors can be included with one or more of the metal precursors, or one or more separate phosphorus component precursor impregnation steps can be included between or after the metal precursor impregnation steps. It also is contemplated to impregnate either the porous refractory inorganic oxide matrix component or the zeolitic component with precursors to the active metallic component and blend the result with the other component. The mechanics of impregnating a support with metallic component precursors are well known to persons skilled in the art and typically involve contacting a support with one or more solutions of one or more precursors in amounts and under conditions effective to yield a final composition containing the-desired amount of metal or metals. Suitable solvents for the impregnating solution or solutions include water and various low boiling alcohols in which the precursors are soluble. Water is preferred over alcohols from the standpoint of cost. In the case of simultaneous impregnations of metal and phosphorus component precursors a more preferred solvent is aqueous phosphoric acid. Metal precursors useful in preparation of the invented catalytic compositions are well known to persons skilled in the art and include a wide range of salts and compounds of the metals that are soluble in the impregnating solvent and convertible to the desired form on calcination. Examples of useful salts include organic acid salts such as acetates, formates and propionates; nitrates; anhydrides; sulfates; and ammonium salts. Useful precursors to the oxygenated phosphorus component are materials capable of reaction with the metal or metals of the metallic component, or compounds of such metal or metals, or precursors thereto, so as to incorporate into the metallic component or metallic component precursor a phosphorus -containing species that can be converted to an oxygenated phosphorus component. From the standpoint of maximizing the promotional effect of the oxygenated phosphorus component, the preferred phosphorus component precursor is one containing or capable of liberating phosphate anions as these are sufficiently reactive with the metal or metal precursors to yield the desired promotional effect. Specific examples of such phosphorus anion sources include phosphoric acid and salts thereof such as ammonium dihydrogen phosphate and diammonium hydrogen phosphate. Other phosphorus component precursors contemplated according to the invention, though less preferred from the standpoint of attaining maximum promotional effect, include organophosphorus compounds such as partial and full esters of the aforesaid oxyacids such as organophosphates and organophosphites; other organophosphorus compounds such as phosphines; and other phosphoric oxyacids such as phosphorus and phosphinic acids. Impregnation of the support component with precursors to the metallic component is conducted under conditions effective to avoid substantial destruction of crystallinity of the crystalline molecular sieve zeolite component. Preferably, such conditions include a temperature that is high enough to maintain the metal and/or phosphorus component precursors in solution in the impregnating solvent though not so high as to decompose such precursors or have substantial adverse effects on the support component. More preferably, impregnating temperatures range from 4.5 to 939C (40 to 2000F). pH of the impregnating solution or solutions to be used also is important from the standpoint of insuring retention of substantial zeolite crystallinity when phosphoric acid or other phosphate anion source is employed as a phosphorus component precursor and/or impregnating solvent. In- such cases, pH preferably is sufficiently high that only insubstantial destruction of zeolite crystallinity takes place during the preparation Of course, the precise pH at which substantial decomposition of crystallinity will occur will vary somewhat depending upon the choice of zeolite component In general, however, pH should be above 2 in order to insure retention of sufficient zeolite crystallinity to insure desirable catalytic performance Most preferably, pH ranges from 2.5 to e in order to insure retention of a high degree of zeolite crystallinity while also insuring the desired association of the phosphorus and metal components of the active metallic component. Following impregnation of the support component with metallic component precursors, it is prefered to dry the impregnated support. It also is contemplated to dry the support subsequent to any intermediate impregnating steps in a multistep impregnation. Preferred drying temperatures range from 27 to 1770C ( & to 3500F), with preferred drying times ranging from a few seconds in spray drying operations to several hours in conventional driers. Following impregnation of the support with precursors to the metallic component and any optional drying steps, the impregnated support is subjected to calcination in order to convert at least a portion of the metal or metals of the metallic component to the active form and to convert phosphorus precursors to oxygenated phosphorus component. Calcination is conducted in an atmosphere containing molecular oxygen at a temperature and for a period of time effective to attain the desired conversion. Preferably, calcination temperatures range from 427 to-6490C (800 to 1,2000F). Preferred calcination times range from 1/2 to 16 hours. As a result of the above-described preparation, there is attained a catalytic composition comprising (1) a metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component, and (2) a support component comprising at least one nonzeolitic, refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component. Preferred compositions are those in which the zeolite component exhibits at least 40% crystallinity as compared to compositions identical but for inclusion of phosphorus component. More preferably, such relative crystallinity is at least 75% in order to ensure desirable catalyst performance. The compositions of this invention have utility in a wide range of hydrocarbon conversion processes in which a chargestock comprising hydrocarbon is contacted with the catalyst under hydrocarbon conversion conditions. The invented catalysts are particularly useful in processes for hydrogen processing of hydrocarbon feed materials such as whole petroleum or synthetic crude oils, coal or biomass liquids, and fractions thereof. The process of the invention is described in further detail with reference to hydrogen processing of such feed materials. Petroleum and synthetic crude oil feeds that can be hydrogen processed according to this aspect of the invention include whole petroleum, shale and tar sands oils, coal and biomass liquids and fractions thereof such as distillates, gas oils and residuals fractions Such feed materials are contacted with the catalyst of the invention under hydrogen processing conditions which will vary depending upon the specific feed to be processed as well as the type of processing desired. Broadly, hydrogen treating temperatures r2r.ge from 177 to 4550C (350 to 8500F), hydrogen pressures range from 0.69 to 20.7 MPa (100 to 3000 psiq) and feed linear hourly space velocities range from 0.1 to 10 volumes of feeci per volume of catalyst per hour. Hydrogen addition rate generally ranges from 36 to 4450 m3/ 3 ( 200 to 25,000 standard cubic feet per barrel (SCFB)). Hydrocarbon feed materials treated under mild hydrocracking conditions are whole petroleum or synthetic crude oils, coal or biomass liquids, or fractions thereof. Substantial levels of impurities such as nitrogen, sulfur, oxygen and/or waxy components may be present in the feeds. Typical feeds contain up to 1,5 wt.t nitrogen and/or oxygen, up to 12 wt% sulfur and/or sufficient waxy components, e.g., n-paraffins and isoparaffins, to exhibit pour points of at least -10C (300F). Specific examples of useful feeds include heavy and light vacuum gas oils, atmospheric and vacuum distillates and deasphalted and hydrotreated residual fractions. Mild hydrocracking conditions vary somewhat depending on the choice of feed as well as the type of processing to be conducted. Dewaxing mild hydrocracking conditions are employed when it is desired to reduce n-paraffin and isoparaffin content of the feed without substantial cracking of desirable aromatics, naphthenes and branched paraffins. Dewaxing mild hydrocracking conditions preferably include a tempt rature of 343 to 4270C, t650 to"e000F), hydrogen pressure of 5.5 to 17.3 I.Pa (800 to 2500 psi) , linear hourly space velocity (LHSV) of 0.2 to 5 and hydrogen addition rate of 178 to 3560 M3/m3(l000 to 20,000 standard cubic feet per barrel (SCFB)). The catalytic dewaxing mild hydrocracking process can be included as part of a multistep process for preparation of lube oils wherein catalytic dewaxing is conducted in combination with other conventional processing steps such as solvent extraction, solvent dewaxing, hydrocracking or hydrotreating to obtain lube oil base stocks of relatively low pour point and high viscosity index and stability. According to a preferred aspect of the invention, however, there is provided an improved process for preparation of lube oil base stocks of high viscosity index, low pour point and sufficiently low sulfur and/or nitrogen content to exhibit good stability consisting essentially of catalytically dewaxing a feed, and preferably a petroleum or synthetic crude oil distillate fraction having a pour point of 10 to 650C (50 to 1500F) and containing up to 5 wt%: sulfur, 0.5 wt.% oxygen and/or 0.5 wt% nitrogen in the presence of the aforesaid catalyst. Conditions according to this aspect of the invention typically are somewhat more severe than those in catalytic dewaxing operations conducted as part of a multi step process. Preferred conditions according to this aspect of the invention include temperature ranging from 370 to 4270C, 700 to 800OF,, pressure of 8.3 to 13.8 MPa (1200 to 2000 psi), LHSV of 0.2 to 2 reciprocal hours and hydrogen addition rate o 356 to 1780 m /m3 (2000 to 10,000 SCFB). A preferred catalyst according to this aspect of the invention is one in which the shape selective zeolitic cracking component is a crystalline borosilicate component of the AMS-lB type in hydrogen form, and the hydrogenating metal of the active metallic component comprises a molybdenum component and a nickel component. Catalytic cracking feed mild hydrocracking conditions are employed when it is desired to remove nitrogen and/or sulfur from the feed as well as crack hydrocarbon components thereof to lower boiling components. Such conditions include temperatures ranging from 343 to 4050C (650 t- 7600F), hydrogen pressures ranging from 3.45 to 13.8 MPa (500 to 200C psi), LHSV ranging froa 0.2 to 4 reciprocal hours and hydrogen addition rates ranging from l to 3560 m3/m3 (1000 to 20,000 SCFB). Preferred catalytic crackinq feed mild hydrocracking conditions include a temperature rangin7 from 365 to 3950C (690 to 7400F)j hydrogen pressure of 5.5 to 11 MPa (800 to 1600 psi), LHSV of O.5 to 1 reciprocal hour anu hydrogen addition rate of 178 to 26;0 m3 3 (1000 to 15,000 SCB). The process can be conducted in either fixed or expanded bed operations using a single reactor or series thereof as desired. Catalysts that are preferred for use in the mild hydrocracking process of the present invention are those in which the active metallic component comprises at least one metal of Group VIB or 'VIII, the non-zeolitic matrix component comprises alumina or silica-alumina and the shape selective crystalline molecular sieve zeolite component comprises a crystalline aluminosilicate zeolite of the ZSM-type or a crystalline borosilicate zeolite of the AMS-type, as these exhibit high activity for hydrogenation and cracking. More preferably, the hydrogenation metal of the active metallic component is nickel, cobalt, chromium, molybdenum or tungsten or a combination thereof and is present in an amount ranging from 10 to 30 wt% calculated as metal oxide and based on total catalyst weight. Preferred support compositions contain 60 to 90 wt% alumina or silica-alumina having dispersed therein 10 to 40 wt% shape selective crystalline molecular sieve zeolite. Most preferably, the hydrogenating metal of the active metallic component of the catalyst employed comprises a combination of nickel and molybdenum. Best results in terms of mild hydrocracking are attained using catalysts containing 1 to 7 wt% NiO, 10 to 20 t% Mo03, 0.1 to 5 wt% oxygenated phosphorus component, calculated as P205, and a support comprising 65 to 85 wt% alumina having dispersed therein 15 to 35 wtZ crystalline borosilicate zeolite of the AMS-type, especially HAMS-lB. Hydrocarbon feed materials treated under hydrocracking conditions are gas oil boiling range hydrocarbons derived from petroleum or synthetic crude oils, coal liquids or biomass liquids. Preferred feeds are those boiling from 205 to 5380C (400 to ,10000F) and containing up to 0.1 wt% nitrogen and/or up to 2 wt% sulfur. Specific examples of preferred gas oil boiling range feeds include petroloul,l and synthetic crude oil distillates such as catalytic cycle oils, virgin gas oil boiling range hydrocarbons and mixtures thereof. Hydrocracking conditions vary somewhat depending on the choice of feed and severity of hydrocracking desired. Broadly, conditions include temperatures ranging from 343 to 4550C (650 to 850OF), total pressures ranging from 6.9 to 20.7 MPa rl000 to 3000 psi3, hydrogen, partial pressures ranging from 2.07 to 17.25 MPa (300 to 2500 psi),linear hourly space velocities (LHSV) ranging from 0.2 to 10 reciprocal hours and hydrogen recylce rates ranging from 890 to 3560 m3,m3 t5,000 to 20,000 SCFB) Hydrogen consumption broadly ranges from 90 to 534 m3/m (500 to 3000 SCFB) undersuchcondi- tions. Preferred conditions in hydrocracking of catalytic cycle oils, virgin gas oils, and combinations thereof to gasoline boiling range products include a temperature ranging from 357 to 4130C (675 to 775n e), total pressure of 10.3 to 17.25 MPa (1500 to 2500 psi), hydrogen partial pressure of 6.9 to 10.35 MPa (1000 to 1500 psi)1space velocity of 0.5 to 4 reciprocal hours and hydrogen recycle rate of 1780 to 2670 m3/m3 (10,000 to 15,000 SCFB), with hydroc,en consumption ranging from 178 to 356 m3/m3 (1000 to 2000 SCFB) The process can be conducted in either fixed or expanded bed operations using a single reactor or series thereof as desire, Catalysts that are preferred for use in the hydrocracking process of the present invention are those in which the active metallic component comprises at least one metal of Group VIB or VIII, the nonzeolitic matrix component comprises alumina, or silica-alumina and the crystalline molecular sieve zeolite component comprises a low sodium, ultrastable Y-type crystalline aluminosilicate zeolite, as these exhibit high activity for hydrogenation and cracking over prolonged periods of time. More preferably, the hydrogenation metal of the active metallic component is nickel, cobalt, chromium, molybdenum or tungsten or a combination thereof and is present in an amount ranging from 8 to 25 wtt, calculated as metal oxide and based on total catalyst weight. Preferred suPport compositions contain 40 to 80 wt% alumina or silica-alumina having dispersed therein 20 to 60 wtZ low sodium, ultrastable Y-type crystalline"alumino silicate zeolite. Most preferably, the hydrogenating metal of the active metallic component of the catalyst employed comprises a combination of cobalt and molybdenum, nickel and molybdenum or nickel and tungsten. Best results are attained using catalysts containing 0.5 to 6 wt% oxygenated phosphorus component, calculated as P2O5 and a hydrogenating component containing 1 to A wit , CoO or NiO and 8 to 15 wt MoO3; or 1 to about 4 wt% NiO and 15 to 25 wtZ W03; ; and a support comprising 50 to 70 wt% alumina or silica-alumina having dispersed therein 30 to 50 wt% low sodium ultrastable Y-type crystalline aluminosilicate zeolite component, such weight percentages of hydrogenating metal oxides being based on total catalyst weight, and such matrix and zeolite weight percentages being based on support weight. Hydrocarbon feeds treated under denitrogenation, hydroreating or hydrocracking conditions are those containing substantial levels of nitrogen compounds. Preferred feeds are those containing at least 0.4 wt% nitrogen. Specific examples of preferred high nitrogen feeds include whole shale oils and fractions thereof such as shale oil resids, vacuum and atmospheric distillates and naphtha fractions. Whole petroleum crude oils, tar sands oils, coal and biomass liquids suitably high in nitrogen, as well as various fractions thereof, also are particularly well suited for use. Denitrogenation conditions vary somewhat depending on the choice of feed as well as the type of processing to be conducted. Denitrogenation hydrotreating conditions are employed when it is desired to reduce nitrogen content of the feed without substantial cracking thereof and include a temperature of 343 to 4050C (650 to 760OF), hydrogen pressure of 6.9 to 17.25 iilPa (1000 to 2500 psi), linear hourlyspace velocity (LHSV) of 0.2 to 4 volumes of feed per volume of catalyst per hour (hour1) and hydro3eflac2itionrateof 356 to 3560 m.3/m3 (2000to 20,000 standard cubic feet per barrel (SCFB). Preferred denitrogenation hydrotreating conditions include a temperature ranging from 360 to 3990C (680 to 7500F), hydrogen pressure of 9.7 to 15.2 MPa L1400 to 2200 psi), LHSV of 0.3 to 3 and hydrogen rate of 712 to 1780 m /m (4000 to 10,000 SCFB) as these result in desirable reductions in product nitrogen while avoiding exposure of the catalyst to conditions so severe as to adversely affect catalyst lifetime. Denitrogenation hydrocracking conditions are employed when it is desired to remove nitrogen from the feed as well as crack higher boiling components thereof to lower boiling components. Denitrogenation hydrocracking temperature ranges from 382 to 4380C (720 to 8200F), hydrogen pressure ranges from 6.9 to 17.25Mpa (1000 to 2500 psi), LHSV ranges from 0.2 to 3 and. hydrogen addition rate ranges from 12 to 3560 m3/m3 (4,000 to 20,000 SCFB). A particularly preferred application in which denitrogenation hydrocracking conditions are employed is in conversion of whole shale oils or fractions thereof to jet fuel Preferred conditions for such an application include a temperature ranging from 399 to 4380C (750 to 3200F), hydrogen pressure of 8.3 to 15.2 MPa (1200 to 2200 psi), LHSV of 0.3:to 1 and hydrogen addition rate of 890 to 1780 m3/m3 (5000 to 10,000 SCFB). The process can be conducted in either fixed or expanded bed operations using a single reactor or. series thereof as desired. Catalysts that are preferred for use in the denitrogenation hydrotreating or hydrocracking process are those in which the hydrogenating metal of the active metallic component is nickel, cobalt, chromium, molybdenum, tungsten or a combination thereof, the non-zeolitic matrix component comprises alumina or silica-alumina and the crystalline molecular sieve zeolite component comprises an ultrastable Ytype crystalline aluminosilicate zeolite, a crystalline aluminosilicate zeolite of the ZSM-type or a crystalline borosilicate zeolite of the AMS-type, as these exhibit high activity for denitrogenation hydrotreating and hydrocracking. More preferably, the hydrogenation metals of the active metallic component comprise a combination of nickel and molybdenum or a combination of cobalt or nickel, chromium and molybdenum and are present in an amount ranging from 10 to 30 wtZ calculated as metal oxide and based on total catalyst weight, and the support component contains 40 to 80 wtt alumina or silica-alumina having dispersed therein 20 to 60 wt crystalline molecular sieve zeolite component, such weight percentages being based on support weight. Most preferably, the catalyst employed in the denitrogenation process contains 1 to 5 wt% NiO and 12 to 20 wtG MOO3; or 1 to 5 wtt CoO or NiO, 2 to 10 wt% Cr203 and12 to 20 wt% Mo03; and 0.5 to 8 wt oxygenated phosphorus COill- ponent, expressed as P205; and a support containing a dispersion of 30 to 60 t% ultrastable Y-type crystalline aluminosilicate zeolite, AMStype crystalline borosilicate zeolite or ZSM-type crystalline: aluminosilicate zeolite in 40 to wti wt% alumina or silica-alumina. Ultrastable Y-type crystalline aluminosilicate zeolites give best results in denitrogenation hydrocracking applications. The present invention is described in further detail in the following examples, it being understood that the same are for purposes of illustration and not limitation. EXAMPLE 1 A support component containing 30 wt.% ultrastable Y-type crystalline aluminosilicate zeolite obtained from the Davison Chemical Division of W. R. Grace and Co. dispersed in 70 wt.% alumina was prepared by mixing 15,890 g alumina sol (10.0 wt.% alumina dry weight) with 681 g ultrastable Y-type zeolite. To the result was added a solution of 400 ml water and 400 ml concentrated NH40H while stirring rapidly to form a gel. The resulting gel was dried overnight at 1210C (2500F) in air, ground to 100 mesh,mulledwith water, extruded to 1.98 mm (5/64") particles, dried overnight at 1210C (2500F) in air-an calcined at 5380C (10000F) in air for three hours. A solution prepared by dissolving 8.30 g (NE4)2cr2o7 in. 49 ml water was added to 72.77 g of support component and allowed to stand for 1 hour after which the result was dried in air at 1210C (2500F) for 1 hour. Subsequently, 18.40 g (NH4)6Mo7024.4H20, 5.85 g Co(N03)2.6H20 and 8.6 g 85%. phosphoric acid (H3P04) were dissolved in 35 ml water to form an impregnating solution having a pH of 3. The impregnating solution was added to the chromia-impregnated support and the mixture was allowed to stand for 1 hour after which the result was dried in air at 1210C (2500F) for 1 hour and calcined in air at5280C (10000F) for 1- hour. The resulting catalyst contained 5.0 wt% Cr203, 15.0 wt.% Mo03, 1.5 wt.% CoO and 5.5 wt.% oxygenated phosphorus component, calculated as P2O. EXAMPLE 2 A support component containing 50 wt.% ultrastable Y-type crystalline aluminosilicate zeolite (Davison) dispersed in 50 wt.% alumina was prepared substantially according to the procedure of Example 1 using 3863 g alumina sol (10 wt.% alumina) and 386.5 g ultrastable Y-type zeolite. A solution prepared by dissolving 16.6 g (NH4)2Cr207 in 90 ml water was added to 148.98 g of the support component and allowed to stand for 1 hour. The result was dried in air at 1210C (2500F) for 1 hour and calcined in air at 5380C (10000F) for 1 hour. Subsequently, 36.8 g (NH4)Mo7024-4H2O, 11.70 g Co(N03)2.6H20 and 13.02 g 85% H3PO4 were dissolved in 67 ml water to form an impregnating solution having a pH of 3 This solution was added to the chromia-impregnated support and the result was allowed to stand for 1 hour after which the result was dried in air at 1210C (2500F) for 1 hour and calcined in air at 5380C (10000F) for 1 hour. The resulting catalyst contained 5.0 wt.% Cr203, 15.0 wt.% MoO3, 1.5 wt.% CoO and 4.0 wt.t oxygenated phosphorus component, calculated as P25. EXAMPLE 3 An impregnating solution having a pH of 5.0 was prepared by dissolving 34.80 g cobalt nitrate, 42.45 g ammonium molybdate and 16.63 g phosphoric acid in 600 ml distilled water, after which total volume of the solution was brought to 660 ml with distilled water. The impregnating solution was added to 331 g of a premixed support component containing 41 wt.% ultrastable Y-type crystalline aluminosilicate zeolite and 59 wt.% silica-alumina and stirred vigorously for a short time. The result was dried in air at 1210C (2500F) for severalhours,ground to pass a 28 mesh screen, formeainto3.18mm (1/8') pellets and calcined in air for 1 hour at 26000 (5000F), forl hour at 3990C (7500F) and for 5 hours at 5380C (10000F). The resulting catalyst contained 9.13 w+.t MoO3, 2.36 wt.% CoO and 2.3 wt.% phosphorus component, calculated as P2O5. EXAMPLE 4 A support component containing 35 wit.8 ultrastable Y-type crystalline aluminosilicate zeolite (Davison) dispersed in 65 wt.% silica-alumina containing 71.7 wt.% silica was prepared in two batches by blending 4160 g of silica-alumina slurry containing about 2.5 wt.% solid with 54.4 g of the zeolite component for 5 to 10 minutes and then filtering, drying the solid in air at 1210C (250 F) overnight, grinding the dried solid to pass through a 30-mesh screen and calcining in air at 538 C (10000F) for 3hours. An impregnating solution was prepared by dissolving 35.4 g cobalt nitrate, 41.6 g ammonium molybdate and 4.6 g phosphoric acid in.472 ml distilled water 290 g of the support component were contacted with the impregnating solution after which the result was dried in air- at 121 C (25O0P) overnight, ground to 28 mesh, formed into 3.18mm(1/8")pills andcalcined in air at 260 C (5000F) forlhour,at3700C (700 F) for 1 hour and at 538 C (10000F) for 5 hours The resulting catalyst contained 2.6 wt.% CoO, 9.6 wt.% MoO3 and 0.6 wt.% oxygenated phosphorus component, calculated as P205. EXAMPLE 5 147.84 g support component containing 20 wt.% AMS-type crystalline borosilicate zeolite dispersed in 80 wt.8 alumina was impregnated with a solution prepared by dissolving 22.09 g (NH4)2M07024.4H20 and 13.63 g Ni(N03)2.6H2O in 68 ml distilled water and adding dropwise 7.44 g 85% H3PO4 thereto while stirring. A small amount of water was added to the impregnation mixture and the result was allowed to stand for 1 hour. The result was dried in air at 1210C (2500F) overnight, and then impregnated with 22.09 g (NH4)2M07024.4H20, 13.63 g Ni(N03)2.6H20, and 7,44 g 85% H3PO4 in 68 ml distilled water. The result was allowed to stand for 2 hours, dried in air at 121 C (2500F) and calcined at 5380C (10000F). The resulting catalyst contained 17.70 wt.% MoO3, 3.44 wt.% NiO and 4.35 wt.% oxygenated phosphorus component, calculated as P205, and had a surface area of 242 mê/g and pore volume of 0.4802 cc/g. EXAMPLE 6 The catalysts prepared in Examples 1 and 2 were tested for denitrogenation and hydrocracking activity in an automated processing unit that included a vertical, tubular, downflow reactor having a length of 83..3cm (32") anuinnerdiameter of 6.35mm (lj4")...Theunit included automatic controls to regulate hydrogen pressure and flow, temperature and feed rate. Catalyst was ground to 14-20 mesh and loaded into a 25.4-30.5cm tl0-l2") segment of the reactor and sulfided therin by passing, 8 vol.% d25in hydrogen over the catalyst at 2.07MPa (300 psi) for 1 hour. and at 14 9 OC (3000F) followed by 1 hour at 205OC(400OF) and then 1 hour at 370 C (700 F). The reactor then was heated to operating temperature, pressured with hydrogen and a high nitrogen feed generated in situ from oil shale was pumped into the reactor using a Ruska pump. The feed had the following properties: API Gravity ( ) 23.8 Nitrogen (wt.%) 1.27 Sulfur (wt.%) 0.65 Oxygen (wt.%) 1.40 Pour Point ( C) lS.50C '(600F) Simulated Distillation (8) IBP--1820C (3600F) 2.0 182--3430C (360-6500F) 42.5 343 C + (650 F+) 55.5 Operating conditions and results for each run are shown in Table I. In addition to runs with the catalysts from Examples 1 and 2, comparative runs were conducted using comparative catalysts A-C which were prepared according to the general procedure of Examples 1 and 2 but without the use of phosphoric acid in the case of A and B and without a zeolite component in the case of C. Compositions of catalysts A-C were as follows: A) 10.0 wt.% Cr203, 15.0 wt.% MoO3 and 1.5 wt.% CoO supported on a dispersion of 30 wt.% ultrastable Y-type crystalline aluminosilicate zeolite (Davison) in 70 wt.% alumina; B) 10.0 wt.% Cr203, 15.0 wt.% MoO3 and 1.5 wt.% CoO supported on a disperson of 50 wt.% ultrastable Y-type crystalline aluminosilicate zeolite dispersed in 50 wt.t alumina; C) 5.0 wt.% Cr203, 15.0 wt.% MoO3, 1.5 wt.% CoO and 4.6 wt.% oxygenated phosphorus component, calculated as P205, supported on alumina. TABLE 1 Catalyst 1 A 2 B C Temp (OC) 405 405 416 416 405 Temp(0F) (760) (760) (78C) (733) (760-) Pressure (MPa) 12 12 12 ' 12 12 Pressure (psi) 1800 1800 1800 1800 1800 LHSV (hour'l) 0.5 0.5 0.5 0.5 0.5 Days on Oil 6 9 7 6 6 Liquid Product (g) 184 239 124 190 198 API Gravity (0) 4D.0 36.5 49.4 49.6 37.0 Pour Point (OC) 21 27 -40 -26 24 Pour Point (OF) (10) (80) -40 (-15) (75) Sulfur (ppm) 2 110 6 262 57 Nitrogen (ppm) 1.7 173 0.7 3 85 Simulated Distillation (%) IBP--1770C (IBP--3500F) 14.5 10.7 44.5 42.0 9.0 177--3430C (350--6500F) 60.0 54.3 53.0 52.6 55.0 343 C (650 F+) 25.5 35.0 2.5 5.4 36.0 As can be seen from the table, catalysts 1 and 2 according to the invention exhibited superior denitrogenation and desulfurization activity as compared to all three comparative catalysts. Further, cracking activities of catalysts 1 and 2 were superior to those of comparative catalysts A and B, respectively, as evidenced by the simulated distillation data showing reduced343 CI(650 Ot'T ) content. Cracking activities of 1 and 2 also were superior to that of catalyst C which lacked a zeolite component. EXAMPLE 7 The catalysts prepared in Examples 3 and 4 were tested for hydrocracking activity in a vertical, tubular, downf low reactor having a length of49.5cm (19-1/2") and inner diameter of 1.39cm (0.55") and equipped with a pressure gauge and DP cell to control hydrogen flow and a high pressure separator for removal of products. The reactor was loaded with 18.75 g catalyst, immersed in a molten salt-containing heating jacket at2600C (5000F) and pressured tb 8 .6MPa (1250 psi) with hydrogen. Temperature was held at 2600C (5000F) for two hours and then feed was pumped to the reactor with a Milton Roy pump. Temperature was slowly increased to 360"C (6800F),held there overnight and then raised to operating temperature of 377-3880C (710-7300F),. Feed rate (LHSV) was 1-2 1. Runs were conducted for two weeks with periodic sampling. The feed used in all runs was a mixture of 70 wt.% light catalytic cycle oil and 30 wt.% light virgin gas oil having the following properties: API Gravity (0) 25.3 Nitrogen (ppm) 304 Sulfur (wt.%) 1.31 Initial Boiling Point (OC) 207 (4040F) Final Boiling Point (OC) 356 (6730F) In addition to the runs conducted using the catalysts of Examples 3 and 4, comparative runs were conducted using comparative catalysts A-C which are described below: : A) 2.5 wt.% CoO and 10.2 wt.% MoO3 supported on a dispersion of 35 wt.% ultrastable Y-type crystal line aluminosilicate zeolite in 65 wt.% alumina prepared substantially according to the procedure of Example 3; B) commercial hydrocracking catalyst containing 2.63 wt.% CoO and 10.5 wt.% MoO3 supported on the base used in Example 3 obtained from the Davison Chemical Division of W. R. Grace and Cho., C) 2.6 wt.% CoO and 10.0 wt.% MoO3 supported on a dispersion of 35 wt.% ultrastable Y-type crystalline aluminosilicate zeolite (Davison) in 65 wt.% alumina and prepared substantially according to the procedure- of Example 4. Hydrocracking activities of the catalysts were determined on the basis of temperature required to convert 77 wit.* of the feed to gasoline boiling range products (up to 1930C (3'800F). Activities relative to comparative catalyst C are reported in Table 2. TABLE 2 CATALYST RELATIVE ACTIVITY INCREASE (%) A 102 2 B 126 26 3 144 44 C 100 4 138 38 As can be seen from the table, the phosphoruspromoted, zeolite-containing-catalysts of the invention exhibited significantly improved hydrocracking activity as compared to the comparative catalysts. EXAMPLE 8 Activity of the catalyst of Example 5 for mild hydrocracking was tested in an automated pilot plant consisting of a downf low, vertical pipe reactor of 76.2cm (30") length and 9;53mum (3/8") inner diameter equipped with four independently wired and controlled heaters, a pressure step down and metering device for introduc tion of hydrogen and an outlet pressure control loop to control withdrawal of hydrogen. The catalyst of Example 5 was calcined in air at 5380C (10000F) fpr 2 hours and then screened to 14-20 mesh. The reactor was loaded to a height of 30.48cm (twelve inches) with glass balls after which 25cm (ten inches) were loaded with 16 cm3 of catalyst. Glass balls were added to fill the reactor. The reactor was heated to 149 C (3000F) and a gaseous mixture of 8 volt H25 in hydrogen was passed over the catalyst at 1.4MPa (200 psi) anu6.29 cc/sec(0.8 ft3/hr).After an hour, temperature was raised to 205 OC (4000F), and after another hour, to 3710C (7000F). After one hour at 3710C (7000F), flow of the gaseous mixture was discontinued and a hydrogen flow of 2136 m3/m (12,000SCkB) at8.3MPa (1200 psi) was begun. Heavy vacuum gas oil was pumped to the reactor at 2.8x10-3 cc/sec (10.2 cc/hr) using a'positive displacement pump. After passage through the reactor, prOduct excited the reactor through a high pressure gas-liquid separator via a valve with a control loop designed to maintain a constant liquid level in the high pressure separator. Feed properties were as follows: API Gravity (0) 18.6 Pour Point (0C) 43 (110 F) Viscosity (cst at 1000C) 11.68 Carbon (wt.%) 84.94 Hydrogen (wt.%) 11.63 Nitrogen (wt.%) 0.166 Sulfur (wt.%) 2.98 Simulated Distillation ( C) (OF) IBP 209 (409) 58 355 671 10% 386 727 20% 420 788 40% 462 863 60% 492 918 80% 525 977 90% 538- 1000+ Paraffins (wt.%) 19.7 19.7 Naphthenes (wt.%) 34.7 34.7 Monoaromatics (wt.%) 12.6 12.6 Polyaromatics and 33.0 33.0 Heterocyclics (wit. In addition to the catalyst from Example 5, a comparative catalyst (A) containing 3.5 wt.% NiO, 10 wt.% Cr203 and 15 wt.% Mo03 supported on a dispersion of 20 wt.% rare earth-exchanged ultrastable Ytype zeolite in 80 wt.% alumina was tested. Another run was conducted using a catalyst (B) containing 20 wt. MoO3, 3.5 wt.% NiO and 3.0 wt.% oxygenated phophorus component, calculated as P205, supported on alumina. Operating conditions and results are shown in Table 3. TABLE 3 RUN NO./SAMPLE NO. 1/1 1/2 1/3 CATALYST 5 5 5 TEMP (OC) 370 393 393 TEMP (OF) (7000F) (740 F) (7400F) PRESSURE (MPa) 8.3 8.3 PRESSURE (psi) (1200 psi) (1200 psi) (1200 psi) LHSV (hour 1) 0.625 0.625 0.625 33 HYDROGEN (m3/m3) 2136 2136 2136 HYDROGEN (SCFB) (12000) (12000) (12000) HOURS ON OIL 136 - 352 496 API GRAVITY (0) 28.0 33.6 32.9 POUR POINT (OC) 27 -57 -51 POUR POINT (OF) (80) (-70) (-60) VISCOSITY (cst at 1000C) 4.71 2.51 2.55 CARBON (wt.%) 87.00 86.90 87.05 HYDROGEN (wt.%) 12.93 13.09 12.94 SULFUR (ppm) 633 137 86 NITROGN (ppm) 135 8.8 14 SIMULATED DISTILLATION (OC) IBP 46 (1140F) -18 (00F) -26(-150F) 5% 165 (3290F) 74 (1650F) 76(1680F) 20% 333 (6310F) 219 (4270F 231(4480F) 50% 425 (7970F) 369 (6960F) 375(7070F) 808 436 (907 F) 460 (8600F) 462(863 F) 95% 532 (9900F) 519(9670F) 516.(9610F) % DESULFURIZATION 97.9 99.5 99.7 % DENITROGENATION 91.9 99.5 99.2 HYDROGEN CONSUMED (m3/m3) 142 186 167 HYDROGEN CONSUMED (SCFB) (795 SCFB) (1045 SCFB) (940 SCFB) YIELD (wt.%) IBP-1820C 5.5 14.8 13.6 (IBP-3600F) 182-3430C 17.9 25.7 24.7 (360-6500F) 3430C (650 F+) 75.4 53.9 55.3 TABLE 3 (Continued) RUN NO./SAMPLE NO. 1/4 1/5 1/6 CATALYST 5 5 5 TEMP ( C) 365 388 388 TEMP ( F) (6900F) (7300F) (7300F) PRESSURE (MPa) 8.3 8.3 8.3 PRESSURE (psi) (1200 psi) (1200 psi) (800 psi) LHSV (hour 1) 0.625 0.625 0.625 HYDROGEN (m /m3) 2136 2136 2136 HYDROGEN (SCFB) 12000 (SCFB) 12000(SCFB) 12000(SCFB) HOURS ON OIL 808 976 1312 API GRAVITY (0) 26.6 30.3 28.2 POUR POINT ( C) 35 -1 13 POUR POINT ( F) (950F) (300F) (550F) VISCOSITY (cst at 1000C) 6.07 3.88 3.89 CARBON (wt.%) 87.09 87.02 87.26 HYDROGEN (wt.%) 12,80 12.96 12.66 SULFUR (ppm) 660 88 368 NITROGEN (ppm) 409 29 338 SIMULATED DISTILLATION ( C) IBP 209(4090F) ND* ND 5% 307(5840F) ND ND 20% 380(7160F) ND ND 50% 443(8300F) ND ND 80% 498(9280F) ND- ND 95% 537(999 F) ND ND % DESULFURIZATION 9 7.7 99.7 98.7 % DENITROGENATION 60.2 98.2 79.6 HYDROGEN CONSUMED (m3/m3) 125 166 113 HYDROGEN CONSUMED (SCFB) (700 SCFB) (930 SCFB) (635 SCFB) YIELD (wt.%) IBP-1820C (IBP-3600F) 0 ND ND 182-3430C (360-6500F) 10.4 ND ND 3430C+ (650 F+) 88.9 ND ND *ND stands for not determined. TABLE 3 (Continued) RUN NO./SAMPLE NO. 2/1 2/2 2/3 CATALYST B B B TEMP (OC) 393 416 416 TEMP (OF) (740) (780) (780) PRESSURE (MPa) 8.3 8.3 8.3 PRESSURE (psi) (1200) (1200) (1200) LHSV (hour ) 0.68 0.68 0.68 HYDROGEN (m /m ) 2136 2136 2136 HYDROGEN (SCFB) (12000) (12000) (12000) HOURS ON OIL 128 320 488 API GRAVITY ( ) ND* 32.5 33.2 POUR POINT ( C) 38 38 32 POUR POINT (OF) (100 F) (1000F) (900F) VISCOSITY (cst at 1000C) ND 2.10 2.30 CARBON (wt.%) 86.78 86.97 87.06 HYDROGEN (wt.%) 13.19 13.02 12.93 SULFUR (ppm) 240 70 16 NITROGEN (ppm) 22 3 1 SIMULATED DISTILLATION ( C) IBP 86 (1870F) 36 (970F) 64 (1470C) 5% 173 (3430F) 118 (2440F) 131 (2670F) 20% 300 (5720F) 227 (4400F) 239 (4620F) 50% 409 (7690F) 347 (656 F) 359 (6780F) 80% 465 (869 F) 442 (8270F) 450 (8410F) 95% 529 (9850F) 499 (9310F) 505 (9410F) % DESULFURIZATION 99.2 99.8 99.9 % DENITROGENATION 98.7 99.8 99.9 HYDROGEN CONSUMED (SCFB) (990) (940) (870) HYDROGEN CONSUMED (m /m ) 176 167 155 YIELD (wt.%) IBP-1820C 5.6 12.0 11.4 (IBP-360 F) 182-3430C 22.9 37.2 34.3 (360-6500F) 3430C+ (6500F+) 70.1 48.0 51.6 *ND stands for not determined. TABLE 3 (Continued) RUN NO./SAMPLE NO. 3/1 3/2 CATALYST A A TEMP ( C) 393 416 TEMP ( F) (740) (780) PRESSURE (MPa) 8.3 8.3 PRESSURE (psi) (1200) (1200) LHSV (hour 1) 0.625 0.625 HYDROGEN m3/m3 2136 2136 HYDROGEN (SCFB) (12000) (12000) HOURS ON OIL 110 158 API GRAVITY (0) 29.7 30.3 POUR POINT ( C) 41 38 POUR POINT ( F) (105 F) (1000F) VISCOSITY (cst at 1000C) 3.84 2.98 CARBON (wto) 87.01 87.16 HYDROGEN (wt.%) 12.97 12.82 SULFUR (ppm) 102 79 NITROGEN (ppm) -76 137 SIMULATED DISTILLATION( C) IBP -13 (90F) 66 (151 F) 5% 184 (364 F) 161 (3220F) 20% 319 (6060F) 292 (5580F) 50% 419 (786 F) 400 (753 F) 80% 485 (905 F) 472 (882 F) 95% 532 (9900F) 520 (9690F) % DESULFURIZATION 99.7 99.1 % DENITROGENATION 95.3 91.6 HYDROGEN CONSUMED (SCFB) (825) (890) HYDROGEN CONSUMED m3/m3 147 158 YIELD (wt.%) IBP-1820C 4.8 6.0 (IBP-360 0F) 182-343 C 20.1 23.3 (360-650 F) 343CC+ (6500F+) 74.0 64.9 *ND stands for not determined. As can be seen from the table, all three catalysts exhibited high desulfurization activity and catalysts 5 and B showed good denitrogenation. Cracking activity, as indicated by the yield data, was generally comparable for catalysts 5 and B, both of which were superior to catalysts A. Catalyst 5 was superior to both comparative catalysts in terms of selective crack'ing of waxy components as evidenced by the reductions in pour point in runs using catalyst 5. Catalyst 5 also was superior in terms of overall performance in that comparable or better results were achieved with that catalyst at lower temperatures than those used in the comparative runs. EXAMPLE 9 A series of catalyst compositions was prepared from various crystalline molecular sieve zeolite and matrix components and aqueous phosphoric acid solutions of various metal salts (pH about 3) according to the general procedure of Examples 1-5. A second series of catalysts was prepared in similar fashion to contain identical levels of metals and support components but no phosphorus (pH about 5). Samples of the catalysts were analyzed by Xray diffraction to determine the effect of phosphoric acid on retention of zeolite crystallinity. For each pair of catalysts (with and without phosphoric and impregnation) of identical metals and support content, intensity of one or more X-ray bands characteristic of the zeolite component and not subject to interference by the metals of the catalysts were measured. For each pair of catalysts, composition and crystallinity of the phosphorus component-containing catalyst relative to that of the phosphorus-free composition is reported in Table 4. TABLE 4 RELATIVE CRYSTAL SAMPLE COMPOSITION (wt.%) LINITY (8) A 3.5% NiO, 18% MoO3, 3.4% P2OS/ 86 50 USY(1), 50% A1203 B 3.5% NiO, 18% MoO3, 3.4% P2O5/ 78 50% y(2), 50% A1203 C 3.5% NiO, 18% MoO3, 3.4% P2O5/ 86 50% ZSM-5(3), 50% A1203 D 1.5% CoO., 10% Cr203, 15% Mo03, 79 4.6% P205/40% HAMS-1B(4), 60% A1203 E 1.5% CoO, 10% Cr203, 15% MoO3, 88 4.6% P205/30% USY, 70% A1203 (1) Ultrastable Y-type crystalline aluminosilicate zeolite. (2) Y-type crystalline aluminosilicate zeolite. (3) Crystalline aluminosilicate zeolite ZSM-5. (4) Crystalline borosilicate zeolite HAMS-lB. As can be seen, crystallinity of the compositions according to the invention was quite high relative to compositions identical but for inclusion of phosphoric acid in preparation. 3.5% NiO, 18.0% MoO3, 3.5% P205/30S USY, 70% A1203 exhibited 66% crystallinity relative to a dispersion of 30% USY in 70% A1203.

Claims: CLAIMS 1. A catalytic c-omposition characterised in that it comprises (1) an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component; and (2) a support component comprising at least one nonzeolitic, porous refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component. 2. The composition of claim 1, further characterised in that the metal having hydrocarbon conversion activity comprises at least one- Group IB, II, IIIB-VIIB or VIII metal. 3. The composition of claim 1 wherein the non-zeolitic, refractory inorganic oxide matrix component comprises aluminia, silica, or a combination of alumina and silica. 4. The composition of claim 1, further characterised in that the crystalline molecular sieve zeolite component comprises at least one crystalline borosilicate zeolite. 5. The composition of claim 1, further characterised in that the crystalline molecular sieve zeolite component comprises at least one crystalline aluminosilicate zeolite. 6. The composition of claim 1, further characterised in that the metal having hydrocarbon conversion activity comprises at least one Group VIB metal. 7. The composition of claim 1, further characterised in that the active metallic component comprises at least one metal having hydrogenation activity. 8. The composition of claim 7 further characterised in that the oxygenated phosphorus component is present in an amount ranging from 0.1 to 20 wt.%, expressed as P205 and based on total weight of the composition. 9. The composition of claim 8, further characterised in that the metal having hydrocarbon conversion activity comprises at least onehydrogenation metal selected from chromium, molybdenum, tungsten, iron, cobalt and nickel. 10. The composition of any of claims 6-9, further characterised in that the crystalline molecular sieve zeolite component comprises at least one crystalline aluminosilicate zeolite selected from ultra-stable Y-type crystalline aluminosilicate zeolites, Y-type crystalline aluminosilicate zeolites in acid form, ZSM-type crystalline aluminosilicate zeolites and mordenite-type crystalline aluminosilicate zeolites. 11. The composition of any of claims 6-9, further characterised in that the crystalline molecular sieve zeolite component comprises at least one crystalline borosilicate zeolite. 12. A catalytic composition comprising (1) an active metallic component comprising from 5 to 35 wt% of at least one hydrogenating metal, and 0.5 to 15 wtZ oxygenated phosphorus component, expressed as P205; and (2) a support component comprising alumina, silica or a combination of alumina and silica and at least one crystalline molecular sieve zeolite component. 13 The catalyst of clam 12, further characterised in that the hydrogenating metal comprises cobalt and molybdenum 14. The catalyst of claim 12 futher characterised in that the hydrogenating metal comprises nickel and molybdenum. 15. The catalyst of claim 12, further characterised in that the hydrogenating metal comprises nickel and tungsten. 16. The catalyst of any of claims 13-15, further characterised in that the hydrogenating metal comprises chromium. 17. A method for preparing a catalytic composition characterised in that a support component comprising at least one non-seolitic, refractory inorganic oxide matrix component and at least one acid-tolerant crystalline molecular sieve zeolite component is impregnated with at least one precursor of an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component under conditions effective to retain substantial zeolite crystallinity; and in that the resulting impregnation product is calcined. 18. The method of claim 17, further characterised in that said precursor of the active metallic component comprises phosphoric acid or a salt thereof having a pH of at least 2, and said support component is impregnated with said phosphoric acid or salt thereof simultaneously with, or subsequent to, impregnation with said at least one metal precrusor. 19. The method of claim 18, further characterised in that said precursor of said active metallic component comprises at least one compound of a Group VIB metal. 20. . The process of claim 19, further characterised in that the Group VIB metal compound and phosphorus component precursor are impregnated simultaneously at a pH of from 2.5 to 6. 21. A hydrocarbon conversion process characterised in that a chargestock comprising hydrocarbon is contacted under hydrocarbon conversion conditions with a catalytic composition comprising (1) an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component, and (2) a support component comprising at least one nonzeolitic, porous refractory inorganic maxtrix component and at least one crystalline molecular sieve zeolite component. 22. A hydrogen processing process characterised in that a whole petroleum of synthetic crude oil, coal or biomass liquid, or a fraction thereof is contacted with hydrogen under hydrogen processing conditions in the presence of a catalytic composition comprising (1) an active metallic component comprising at least one metal having hydrogenation activity and at least one oxygenated phosphorus component, and (2) a support component comprising at least one non-zeolitic, porous refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component

Inventors: BAIRD, MICHAEL JEFFERSON, GUTBERLET, LOUIS CHARLES, HENSLEY, ALBERT LLOYD, JR., HOPKINS, PAUL DONALD, MILLER, JEFFEREY TEMPLETON, NEVITT, THOMAS DICKEY, TAIT, ANDREW MARTIN
Applicants: AMOCO CORPORATION
Application year: 1982
Main classification: B01J27
IPC codes: B01J27, B01J29, C10G49