Hydrocarbon conversion with a multimetallic catalytic composite

The subject of the present invention is a novel acidic trimetallic catalytic composite which has exceptional activity, selectivity, and resistance to deactivation when employed in a hydrocarbon conversion process that required a catalyst having both a hydrogenation-dehydrogenation function and a selective acid or cracking function. More precisely, the present invention involves a novel dual-function acidic trimetallic catalytic composite which beneficially utilizes a catalytic component, bismuth, which traditionally has been thought of and taught to be a poison for a platinum group metal because of its close proximity in the Periodic Table to the notorious platinum poison, arsenic. Bismuth is utilized in the present invention to interact with a platinum or palladium- and rhodium-containing acidic catalyst to enable substantial improvements in hydrocarbon conversion processes of the type that have traditionally utilized platinum group metal-containing catalysts to accelerate the various hydrocarbon conversion reactions associated therewith. In another aspect, this invention concerns the improved processes that are produced by the use of an acidic trimetallic catalytic composite comprising a combination of a platinum or palladium component, a rhodium component, a bismuth component, and a halogen component with a porous, high surface area carrier material in a manner such that (1) the platinum or palladium, bismuth, and rhodium components are uniformly dispersed throughout the porous carrier material, (2) the amount of the bismuth component is not greater than the amount of the platinum or palladium component on an atomic basis and (3) substantially all of the platinum or palladium, rhodium, and bismuth components are present therein as the corresponding elemental metals. In a specific aspect, the present invention concerns an improved reforming process which utilizes the subject acidic trimetallic catalyst to markedly improve activity, selectivity, and stability characteristics associated therewith, to increase yields of C.sub.5 + reformate and of hydrogen recovered therefrom and to allow operation thereof at high severity conditions not heretofore generally employed in the art of continuous catalytic reforming of hydrocarbons with a platinum-containing monometallic, dual-function catalyst.
Composites having a hydrogenation-dehydrogenation function and a selective acid or cracking function are widely used today as catalysts in many industries, such as the petroleum or petrochemical industry, to accelerate a wide spectrum of hydrocarbon conversion reactions. Generally, the cracking function is thought to be associated with an acid-acting material of the porous, adsorptive, refractory oxide type which is typically utilized as the support or carrier for a heavy metallic component such as the metals or compounds of metals of the transition elements of Groups V through VIII of the Periodic Table to which are generally attributed the hydrogenation-dehydrogenation function.
These catalytic composites are used to accelerate a wide variety of hydrocarbon conversion reactions such as hydrocracking, isomerization, dehydrogenation, hydrogenation, desulfurization, cyclization, alkylation, polymerization, halogenation, hydrogenolysis, cracking, hydroisomerization, etc. In many cases, the commercial applications of these catalysts are in processes where more than one of these reactions are proceeding simultaneously. An example of this type of process is reforming wherein a hydrocarbon feed stream containing paraffins and naphthenes is subjected to conditions which promote dehydrogenation of naphthenes to aromatics, dehydrocyclization of paraffins to aromatics, isomerization of paraffins and naphthenes, hydrocracking of naphthenes and paraffins, and the like reactions to produce an octane-rich or aromatic-rich product stream. Another example is a hydrocracking process wherein catalysts of this type are utilized to effect selective hydrogenation and cracking of high molecular weight unsaturated materials, selective hydrocracking of high molecular weight materials, and other like reactions, to produce a generally lower boiling, more valuable output stream. Yet another example is a hydroisomerization process wherein a hydrocarbon fraction which is relatively rich in straight-chain paraffin and/or olefinic compounds are contacted with a dual-function catalyst to produce an output stream rich in isoparaffin compounds.
Regardless of the reaction involved or the particular process involved, it is of critical importance that the dual-function catalyst exhibit not only the capability to initially perform its specified functions but also that it has the capability to perform them satisfactorily for prolonged periods of time. The analytical terms used in the art to measure how well a particular catalyst performs its intended functions in a particular hydrocarbon conversion environment are activity, selectivity, and stability. And for purposes of discussion here these terms are conveniently defined for a given charge stock as follows: (1) activity is a measure of the catalyst's ability to convert hydrocarbon reactants into products at a specified severity level where severity level means the reaction conditions used--that is, the temperature, pressure, contact time, and presence of diluents such as H.sub.2 ; (2) selectivity refers to the amount of desired product or products obtained relative to the amount of reactants converted or charged; (3) stability refers to the rate of change with time of the activity and selectivity parameters--obviously, the smaller rate implying the more stable catalyst. In a reforming process, for example, activity commonly refers to the amount of conversion that takes place for a given charge stock at a specified severity level and is typically measured by octane number of the C.sub.5 + product stream; selectivity usually refers to the amount of C.sub.5 + yield that is obtained at the particular severity or activity level relative to the amount of the charge stock; and stability is typically equated to the rate of change with time of activity, as measured by octane number of C.sub.5 + product and of selectivity, as measured by C.sub.5 + yield. Actually, this last statement is not strictly correct because generally a continuous reforming process is run to produce a constant octane C.sub.5 + product with a severity level being continuously adjusted to attain this result; and, furthermore, the severity level is for this process usually varied by adjusting the conversion temperature in the reaction zone so that, in point of fact, the rate of change of activity finds response to the rate of change of conversion temperatures and changes in this last parameter are customarily taken as indicative of activity stability.
As is well known to those skilled in the art, the principal cause of observed deactivation or instability of a dual-function catalyst when it is used in a hydrocarbon conversion reaction is associated with the fact that coke forms on the surface of the catalyst during the carse of the reaction. More specifically, in these hydrocarbon conversion processes, the conditions utilized typically result in the formation of heavy, high molecular weight, black, solid or semi-solid, carbonaceous material which is a hydrogen-deficient polymeric substance having properties akin to both polynuclear aromatics and graphite. This material coats the surface of the catalyst and reduces its activity by shielding its active sites from the reactants. In other words, the performance of this dual-function catalyst is sensitive to the presence of carbonaceous deposits on the surface of the catalyst. Accordingly, the major problem facing workers in this area of the art is the development of more active and selective catalytic composites that are not as sensitive to the presence of these carbonaceous materials and/or have the capability to suppress the rate of formation of these carbonaceous material on the catalyst. Viewed in terms of performance parameters, the problem is to develop a dual-function catalyst having superior activity, selectivity, and stability. In particular, for a reforming process the problem is typically expressed in terms of shifting and stabilizing the C.sub.5 + yield-octane relationship--C.sub.5 + yield being representative of selectivity and octane being proportional to activity.
I have now found a dual-function catalytic composite which possesses improved activity, selectivity, and stability when it is employed in a process for the conversion of hydrocarbons of the type which have heretofore utilized dual-function catalytic composites such as processes for isomerization, hydroisomerization, dehydrogenation, desulfurization, denitrogenization, hydrogenation, alkylation, dealkylation, disproportionation, polymerization, oligomerization, hydrodealkylation, transalkylation, cyclization, dehydrocyclization, hydrogenolysis, cracking, hydrocracking, reforming, hydrogenation, halogenation, and the like processes. In particular, I have ascertained that an acidic trimetallic catalytic composite, comprising a combination of a platinum or palladium component, a bismuth component, a rhodium component, and a halogen component with a porous refractory carrier material can enable the performance of a hydrocarbon conversion process utilizing a dual-function catalyst to be substantially improved, provided the amounts and oxidation states of the metallic components and the distribution thereof in the catalytic composite are carefully controlled in the manner indicated herein. Since the earliest introduction of catalysts containing a platinum group component, it has been axiomatic that the effect of arsenic on a platinum-containing catalyst is detrimental. This concept has become so fixed and certain in the art that tremendous efforts have been devoted to removing arsenic contaminants from charge stocks that are to be processed in a unit containing a platinum catalyst. In addition, the art is replete with a significant number of methods for reactivating a platinum-containing catalyst once it has been deactivated by contact with arsenic or compounds of arsenic. Because bismuth is a member of the same group of the Periodic Table (Group VA) and is known to have similar chemical properties to arsenic, it has fallen into the same category and has been traditionally thought of as a poison for a platinum-containing catalyst. The art has on occassion hinted at or proposed to use the poisoning effect of Group VA metallic elements to modify or attenuate the platinum component of a dual-function catalyst. For examples of these suggestions, reference may be had to the teachings of U.S. Pat. Nos. 3,156,737; 3,206,391; 3,291,755, and 3,511,888. However, the art has not recognized that bismuth can be utilized to promote a platinum-containing catalyst; that is, to simultaneously increase its activity, selectivity, and stability in hydrocarbon conversion service. In particular, the art has apparently never contemplated the use of a platinum-bismuth catalyst in a catalytic reforming process. As a matter of fact, the art on this last process is replete with teachings that contact of the platinum-containing reforming catalyst, with metallic elements of Group VA of the Periodic Table, and particularly arsenic, is to be avoided if at all possible, and if contact occurs to any substantial degree, the catalyst must be immediately regenerated or reactivated by procedures for removal of these detrimental Group VA constituents. In sharp contrast to this historic teaching of the art that bismuth is detrimental to a platinum-containing reforming catalyst, I have now discerned that the presence of bismuth in a catalyst containing a platinum or palladium component and a rhodium component can be very beneficial under certain conditions. One essential condition associated with the acquisition of the beneficial aspects of bismuth with this type of platinum- or palladium-containing catalyst is the atomic ratio of bismuth to platinum or palladium contained in the composite; my findings here indicate that it is only when this ratio is not greater than 1:1 that the beneficial interaction of bismuth with the platinum- or palladium metal and the rhodium metal is obtained. A second condition is the presence of a halogen component; my finding on this matter is that the presence of a relatively small amount of halogen is required to see the beneficial effect. Another condition for achieving this beneficial interaction of bismuth with this type of catalyst is the distribution of the bismuth, rhodium, and platinum or palladium components in the carrier material with which they are combined; my finding here is that it is essential that these components be uniformly dispersed throughout the porous carrier material--that is, the concentration of these components is approximately the same in any reasonably divisible portion thereof. Still another condition for this beneficial effect is the oxidation states of the metallic components; my finding here is that it is essential that the bismuth, rhodium, and platinum or palladium components are present in the composite in the corresponding elemental metallic states. A trimetallic acidic catalyst meeting these essential limitations differs sharply, both in substance and in capabilities from the bismuth- and platinum-containing catalyst that are suggested by the prior art.
In the case of a reforming process, one of the principal advantages associated with the use of the instant acidic trimetallic catalyst involves the acquisition of the capability to operate in a stable manner in a high severity operation; for example, a continuous reforming process producing a C.sub.5 + reformate having an octane of about 100 F-1 clear and utilizing a relatively low pressure of 50 to about 350 psig. In this latter embodiment the principal effect of the bismuth component is to stabilize the platinum or palladium component and the rhodium component by providing a mechanism for allowing them to better resist the rather severe deactivation normally associated with these conditions. In short, the present inveniton essentially involves the finding that the addition of a controlled amount of a bismuth component to a dual-function hydrocarbon conversion catalyst, containing a platinum or palladium component, a rhodium component, and a halogen component, coupled with the uniform distribution of the bismuth component throughout the catalytic composite to achieve an atomic ratio of bismuth to platinum or palladium metal of not greater than 1:1 and with careful control of the oxidation states of the metallic components enables the performance characteristics of the catalyst to be sharply and materially improved.
It is, accordingly, one object of the present invention to provide an acidic trimetallic hydrocarbon conversion catalyst having superior performance characteristics when utilized in a hydrocarbon conversion process. A second object is to provide an acidic trimetallic catalyst having dual-function hydrocarbon conversion performance characteristics that are relatively insensitive to the deposition of hydrocarbonaceous material thereon. A third object is to provide preferred methods of preparation of this trimetallic catalytic composite which insures the achievement and maintenance of its beneficial properties. Another object is to provide an improved reforming catalyst having superior activity, selectivity, and stability when employed in a low pressure reforming process. Yet another object is to provide a dual-function hydrocarbon conversion catalyst which utilizes a relatively inexpensive component, bismuth, to promote and stabilize a platinum or palladium component and a rhodium component. Still another object is to provide a method of preparation of a bismuth-containing trimetallic catalyst which insures the bismuth component is in a highly dispersed metallic state during use in the conversion of hydrocarbons.
In brief summary, the present invention is, in one embodiment, a catalytic composite comprising a porous carrier material containing, on an elemental basis, about 0.01 to about 2 wt. % platinum or palladium, about 0.1 to about 3.5 wt. % halogen, about 0.01 to about 2 wt. % rhodium, and bismuth in an amount sufficient to result in an atomic ratio of bismuth to platinum or palladium of about 0.1:1 to about 1:1, wherein the platinum or palladium, bismuth, and rhodium are uniformly dispersed throughout the porous carrier material, and wherein substantially all of the platinum or palladium, rhodium, and bismuth are present in the corresponding elemental metallic states.
A second embodiment relates to a catalytic composite comprising a porous carrier material containing, on an elemental basis, about 0.05 to about 1 wt. % platinum, about 0.5 to about 1.5 wt. % halogen, about 0.05 to about 1 wt. % rhodium, and bismuth in an amount sufficient to result in an atomic ratio of bismuth to platinum of about 0.1:1 to about 0.75:1, wherein substantially all of the platinum, rhodium, and bismuth are present in the corresponding elemental metallic states, and wherein the metallic ingredients are uniformly dispersed in the porous carrier material.
Another embodiment relates to a catalytic composite comprising a combination of the catalytic composite described in the first or second embodiment with a sulfur component in an amount sufficient to incorporate about 0.01 to about 0.5 wt. % sulfur, calculated on an elemental basis.
Yet another embodiment relates to a process for the conversion of hydrocarbons comprising contacting the hydrocarbon and hydrogen with the catalytic composite described above in the first or second embodiments at hydrocarbon conversion conditions.
A preferred embodiment relates to a process for reforming a gasoline fraction which comprises contacting the gasoline fraction and hydrogen with the catalytic composite described above in the first or second embodiments at reforming conditions selected to produce a high-octane reformate.
Other objects and embodiments of the present invention relate to additional details regarding preferred catalytic ingredients, preferred amounts of ingredients, suitable methods of composite preparation, operating conditions for use in the hydrocarbon conversion processes, and the like particulars which are hereinafter given in the following detailed discussion of each of these facets of the present invention.
The acidic trimetallic catalyst of the present invention comprises a porous carrier material or support having combined therewith catalytically effective amounts of a platinum or palladium component, a bismuth component, a rhodium component, and a halogen component.
Considering first the porous carrier material utilized in the present invention, it is preferred that the material be a porous, adsorptive, high-surface area support having a surface area of about 25 to about 500 m.sup.2 /g. The porous carrier material should be relatively refractory to the conditions utilized in the hydrocarbon conversion process, and it is intended to include within the scope of the present invention carrier materials which have traditionally been utilized in dual-function hydrocarbon conversion catalysts such as: (1) activated carbon, coke, or charcoal; (2) silica or silica gel, silicon carbide, clays, and silicates including those synthetically-prepared and naturally-occurring, which may or may not be acid treated, for example, attapulgus clay, china clay, diatomaceous earth, fuller's earth, kaoline, kieselguhr, etc.; (3) ceramics, porcelain, crushed firebrick, bauxite; (4) refractory inorganic oxides such as alumina, titanium dioxide, zirconium dioxide, chromium oxide, beryllium oxide, vanadium oxide, cerium oxide, hafnium oxide, zinc oxide, magnesia, thoria, boria, silica-alumina, silica-magnesia, chromia-alumina, alumina-boria, silica-zirconia, etc; (5) zeolitic crystalline aluminosilicates such as naturally-occurring or synthetically-prepared mordenite and/or faujasite, either in the hydrogen form or in a form which has been treated with multivalent cations; (6) spinels such as MgAl.sub.2 O.sub.4, FeAl.sub.2 O.sub.4, ZnAl.sub.2 O.sub.4, CaAl.sub.2 O.sub.4, and other like compounds having the formula MO.Al.sub.2 O.sub.3 where M is a metal having a valence of 2; and (7) combinations of elements from one or more of these groups. The preferred porous carrier materials for use in the present invention are refractory inorganic oxides, with best results obtained with a carrier material consisting essentially of alumina. Suitalbe alumina materials are the crystalline aluminas known as the gamma-, eta-, and theta-alumina, with gamma- or eta-alumina giving best results. In addition, in some embodiments, the alumina carrier material may contain minor proportions of other well known refractory inorganic oxides such as silica-zirconia, magnesia, etc.; however, the preferred support is substantially pure gamma- or eta-alumina. Preferred carrier materials have an apparent bulk density of about 0.3 to about 0.9 g/cc and surface area characteristics such that the average pore diameter is about 20 to 300 Angstroms, the pore volume is about 0.1 to about 1 cc/g and the surface area is about 100 to about 500 m.sup.2 /g. In general, best results are typically obtained with a gamma-alumina carrier material which is used in the form of spherical particles having: a relatively small diameter (i.e. typically about 1/16 inch), an apparent bulk denstiy of about 0.3 to about 0.8 g/cc, a pore volume of about 0.4 cc/g, and a surface area of about 175 m.sup.2 /g.
The preferred alumina carrier material may be prepared in any suitable manner and may be synthetically-prepared or natural occurring. Whatever type of alumina is employed, it may be activated prior to use by one or more treatments including drying, calcination, steaming, etc., and it may be in a form known as activated alumina, activated alumina of commerce, porous alumina, alumina gel, etc. For example, the alumina carrier may be prepared by adding a suitable alkaline reagent, such as ammonium hydroxide to a salt of aluminum such as aluminum chloride, aluminum nitrate, etc.; in an amount to form an aluminum hydroxide gel which upon drying and calcining is converted to alumina. The alumina carrier may be formed in any desired shape such as spheres, pills, cakes, extrudates, powders, granules, tablets, etc., and utilized in any desired size. For the purpose of the present invention a particularly preferred form of alumina is the sphere; and alumina spheres may be continuously manufactured by the well known oil drop method which comprises: forming an alumina hydrosol by any of the techniques taught in the art and preferably by reacting aluminum metal with hydrochloric acid, combining the resulting hydrosol with a suitable gelling agent and dropping the resultant mixture into an oil bath maintained at elevated temperatures. The droplets of the mixture remain in the oil bath until they set and form hydrogel spheres. The spheres are then continuously withdrawn from the oil bath and typically subjected to specific aging treatments in oil and an ammoniacal solution to further improve their physical characteristics. The resulting aged and gelled particles are then washed and dried at a relatively low temperature of about 300.degree. F. to about 400.degree. F. and subjected to a calcination procedure at a temperature of about 850.degree. F. to about 1300.degree. F. for a period of about 1 to about 20 hours. This treatment effects conversion of the alumina hydrogel to the corresponding crystalline gamma-alumina. See the teachings of U.S. Pat. No. 2,620,314 for additional details.
One essential ingredient of the present catalytic composite is a rhodium component. It is of fundamental importance that substantially all of the rhodium component exists within the catalytic composite of the present invention in the elemental metallic state and the subsequently described reduction procedure is designed to accomplish this objective. The rhodium component may be utilized in the composite in any amount which is catalytically effective, with the preferred amount being about 0.01 to about 2 wt. % thereof, calculated on an elemental basis. Typically, best results are obtained with about 0.05 to about 1 wt. % rhodium. It is additionally preferred to select the specified amount of rhodium from within this broad weight range as a function of the amount of the platinum or palladium component, on an atomic basis, as is explained hereinafter.
This rhodium component may be incorporated into the catalytic composite in any suitable manner known to those skilled in the catalyst formulation art which results in a relatively uniform distribution of rhodium in the carrier material. In addition, it may be added at any stage of the preparation of the composite--either during preparation of the carrier material or thereafter--and the precise method of incorporation used is not deemed to be critical. However, best results are obtained when the rhodium component is relatively uniformly distributed throughout the carrier material, and the preferred procedures are the ones known to result in a composite having this relatively uniform distribution. One acceptable procedure for incorporating this component into the composite involves cogelling or coprecipitating the rhodium component during the preparation of the preferred carrier material, alumina. This procedure usually comprehends the addition of a soluble, decomposable compound of rhodium such as rhodium trichloride hydrate to the alumina hydrosol before it is gelled. The resulting mixture is then finished by conventional gelling, aging, drying, and calcination steps as explained hereinbefore. A preferred way of incorporating this component is an impregnation step wherein the porous carrier material is impregnated with a suitable rhodium-containing solution either before, during, or after the carrier material is calcined. Preferred impregnation solutions are aqueous solutions of water soluble, decomposable rhodium compounds such as hexammine rhodium chloride, rhodium carbonylchloride, rhodium trichloride hydrate, rhodium nitrate, sodium hexachloromodate (III), sodium hexanitrorhodate (III), rhodium sulfate, and the like compounds. Best results are ordinarily obtained when the impregnation solution is an aqueous solution of rhodium trichloride hydrate or rhodium nitrate. This component can be added to the carrier material either prior to, simultaneously with, or after the other metallic components are combined therewith. Best results are usually achieved when this component is added simultaneously with the other metallic components. In fact, excellent results are obtained, as reported in the examples, with a one step impregnation procedure using an aqueous solution comprising chloroplatinic or chloropalladic acid, rhodium trichloride hydrate, hydrochloric acid, and bismuth trichloride.
A second essential ingredient of the subject catalyst is the platinum or palladium component. That is, it is intended to cover the use of platinum or palladium or mixtures thereof as a second component of the present composite. It is an essential feature of the present invention that substantially all of the platinum or palladium component exists within the final catalytic composite in the elemental metallic state (i.e., as elemental platinum or palladium). Generally, the amount of the second component used in the final composite is relatively small compared to the amount of the other components combined therewith. In fact, the platinum or palladium component generally will comprise about 0.01 to about 2 wt. % of the final catalytic composite, calculated on an elemental basis. Excellent results are obtained when the catalyst contains about 0.05 to about 1 wt. % or platinum or palladium metal.
This platinum or palladium component may be incorporated in the catalytic composite in any suitable manner known to result in a relatively uniform distribution of this component in the carrier material such as coprecipitation or cogellation, ion-exchange, or impregnation. The preferred method of preparing the catalyst involves the utilization of a soluble, decomposable compound of platinum or palladium to impregnate the carrier material in a relatively uniform manner. For example, this component may be added to the support by commingling the latter with an aqueous solution of chloroplatinic or chloropalladic acid. Other water-soluble compounds of platinum or palladium may be employed in impregnation solutions and include ammonium chloroplatinate, bromoplatinic acid, platinum trichloride, platinum tetrachloride hydrate, platinum dichlorocarbonyl dichloride, dinitrodiaminoplatinum, sodium tetranitroplatinate (II), tetrammine-platinum (II) chloride, palladium chloride, palladium nitrate, palladium sulfate, diammine-palladium (II), hydroxide, tetrammine-palladium (II) chloride, etc. The utilization of a platinum or palladium chloride compound, such as chloroplatinic or chloropalladic acid, is preferred since it facilitates the incorporation of both the platinum or palladium component and at least a minor quantity of the halogen component in a single step. Hydrogen chloride or the like acid is also generally added to the impregnation solution in order to further facilitate the incorporation of the halogen component and the uniform distribution of the metallic component throughout the carrier material. In addition, it is generally preferred to impregnate the carrier material after it has been calcined in order to minimize the risk of washing away the valuable platinum or palladium compounds; however, in some cases it may be advantageous to impregnate the carrier material when it is in a gelled state.
Yet another essential constituent of the trimetallic composite of the present invention is a bismuth component. It is an essential feature of the present invention that substantially all of this component is present in the composite as the elemental metal. That is, it is believed to be a prerequisite for the acquisition of the beneficial effect of bismuth on a platinum-containing catalyst that the bismuth component exists in the catalytic composite in the zero oxidation state. All of the methods of preparation of the catalytic composite of the present invention include a substantially water-free prereduction step which is designed to result in the composite containing substantially all of the bismuth component in the elemental metallic state.
The bismuth component may be incorporated into the catalytic composite in any suitable manner known to effectively disperse this component throughout the carrier material or to result in this conditions. Thus, this incorporation may be accomplished by coprecipitation or cogellation with the porous carrier material, ion-exchange with the carrier material while it is in a gel state, or impregnation of the carrier material at any stage in its preparation. It is to be noted that it is intended to include within the scope of the present invention all conventional methods for incorporating a metallic component in a catalytic composite which results in a uniform distribution of the metllic component throughout the associated carrier material. One preferred method of incorporating the bismuth component into the catalytic composite involves coprecipitating the bismuth component during the preparation of the preferred refractory oxide carrier material. Typically, this involves the addition of a suitable, soluble, decomposable bismuth compound or complex to the alumina hydrosol, and then combining the hydrosol with a suitable gelling agent and dropping the resulting mixture into an oil bath as explained in detail hereinbefore. After drying and calcining the resulting gelled carrier material, there is obtained an intimate combination of alumina and bismuth oxide, which combination has the bismuth component uniformly dispersed throughout the alumina. Another preferred method of incorporating the bismuth component into the catalytic composite involves the utilization of a soluble decomposable compound or complex of bismuth to impregnate the porous carrier material. In general, the solvent used in this preferred impregnation step is selected on the basis of its capability to dissolve the desired bismuth compound and is typically an aqueous acidic solution. Hence, the bismuth component may be added to the carrier material by commingling the latter with an aqueous solution of a suitable bismuth salt or water-soluble compound or complex of bismuth such as bismuth ammonium citrate, bismuth tribromide, bismuth trichloride, bismuth trihydroxide, bismuth oxybromide, bismuth oxychloride, bismuth trioxide, bismuth potassium tartrate, bismuth acetate, bismuth oxycarbonate, bismuth nitrate, and the like compounds. Best results are ordinarily obtained with a solution of bismuth trichloride in hydrochloric acid. In general, the bismuth component can be impregnated either prior to, simultaneously with, or after the other metallic components are added to the carrier material. However, I have obtained excellent results by impregnating the bismuth component simultaneously with the platinum or palladium and rhodium components. In fact, I have determined that a preferred impregnation solution contains chloroplatinic acid, rhodium trichloride hydrate, hydrochloric acid, and bismuth trichloride.
Regardless of which bismuth compound is used in the preferred impregnation step, it is important that the bismuth component be uniformly distributed throughout the carrier material. In order to achieve this objective it is necessary to maintain the pH of the impregnation solution at a value less than 3, and preferably less than 1, and to dilute the solution to a volume which is approximately the same or greater than the volume of the carrier material which is impregnated. It is preferred to use a volume ratio of impregnation solution to void volume of carrier material of at least 0.75:1 and preferably about 1:1 to about 3:1 or more. Similarly, a relatively long contact time should be used during this impregnation step ranging from about 0.25 hours up to about 0.5 hours or more. The carrier material is likewise preferably constantly agitated during this impregnation step.
It is essential to incorporate a halogen component into the trimetallic catalytic composite of the present invention. Although the precise form of the chemistry of the association of the halogen component with the carrier material is not entirely known, it is customary in the art to refer to the halogen component as being combined with the carrier material, or with the other indredients of the catalyst in the form of the halide (e.g., as the combined chloride). This combined halogen may be either fluorine, chlorine, bromine, or mixtures thereof. Of these fluorine and, particularly, chlorine are preferred for the purpose of the present invention. The halogen may be added to the carrier material in any suitable manner, either during preparation of the support or before or after the addition of the other components. For example, the halogen may be added, at any stage of the preparation of the carrier material or to the calcined carrier material, as an aqueous solution of a suitable, decomposable halogen-containing compound such as hydrogen fluoride, hydrogen chloride, hydrogen bromide, ammonium chloride, etc. The halogen component or a portion thereof, may be combined with the carrier material during the impregnation of the latter with the metallic components; for example, through the utilization of a mixture of chloroplatinic acid, bismuth trichloride, and hydrogen chloride. In another situation, the alumina hydrosol which is typically utilized to form the preferred alumina carrier material may contain halogen and thus contribute at least a portion of the halogen component to the final composite. For reforming, the halogen will be typically combined with the carrier material in an amount sufficient to result in a final composite that contains about 0.1 to about 3.5% and preferably about 0.5 to about 1.5 % by weight of halogen, calculated on an elemental basis. In isomerization or hydrocracking embodiments, it is generally preferred to utilize relatively larger amounts of halogen in the catalyst--typically, ranging up to about 10 wt. % halogen, calculated on an elemental basis, and more preferably, about 1 to about 5 wt. %. It is to be understood that the specified level of halogen component in the instant catalyst can be achieved or maintained during use in the conversion of hydrocarbons by continuously or periodically adding to the reaction zone a decomposable halogen-containing compound such as an organic chloride (e.g., ethylene dichloride, carbon tetrachloride, t-butyl chloride) in an amount of about 1 to 100 wt. ppm. of the hydrocarbon feed, and preferably about 1 to 10 wt. ppm.
Regarding the preferred amounts of the various metallic components of the subject catalyst, I have found it to be a preferred practice to select the amount of the rhodium component to produce a composite containing an atomic ratio of rhodium to platinum or palladium within the broad range of about 0.1:1 to about 2:1, with the preferred range being about 0.25:1 to about 1.5:1. Similarly, I have found that it is essential to fix the amount of the bismuth component as a function of the amount of the platinum or palladium component contained in the composite. More specifically, I have observed that the beneficial interaction of the bismuth component with the platinum or palladium component is only obtained when the bismuth component is present, on an atomic basis, in an amount not greater than the platinum or palladium component. Quantitatively, the amount of the bismuth component is preferably sufficient to provide an atomic ratio of bismuth to platinum or palladium of about 0.1:1 to about 1:1, with best results obtained at an atomic ratio of about 0.1:1 to about 0.75:1. The criticalness associated with this atomic ratio limitation is apparent when an attempt is made to convert hydrocarbons with a catalyst having an atomic ratio of bismuth to platinum or palladium metal of greater than 1:1. In this latter case substantial deactivation of the platinum or palladium component is observed. Accordingly, it is an essential feature of the present invention that the amount of the bismuth component is chosen as a function of the amount of the platinum or palladium component in order to insure that the atomic ratio of these components in the resulting catalyst is within the stated range. Specific examples of especially preferred catalytic composites are as follows: (1) a catalytic composite comprising 0.375 wt. % platinum, 0.375 wt. % rhodium, 0.25 wt. % bismuth, and 0.5 to 1.5 wt. % halogen combined with an alumina carrier material (atomic ratio Bi to Pt = 0.622:1); (2) a catalytic composite comprising 0.375 wt. % platinum, 0.375 wt. % rhodium, 0.15 wt. % bismuth, and 0.5 to 1.5 wt. % halogen combined with an alumina carrier material (atomic ratio Bi to Pt = 0.38:1); (3) a catalytic composite comprising 0.375 wt. % platinum, 0.2 wt. % rhodium, 0.1 wt. % bismuth, and 0.5 to 1.5 wt. % halogen combined with an alumina carrier material (atomic ratio Bi to Pt = 0.25:1); (4) a catalytic composite comprising 0.375 wt. % platinum, 0.375 wt. % rhodium, 0.5 wt. % bismuth, and 0.5 to 1.5 wt. % halogen combined with an alumina carrier material (atomic ratio Bi to Pt = 0.126:1); and, (5) a catalytic composite comprising 0.75 wt. % platinum, 0.1 wt. % rhodium, 0.4 wt. % bismuth, and 0.5 to 1.5 wt. % halogen combined with an alumina carrier material (atomic ratio Bi to Pt = 0.5:1).
Another significant parameter for the present catalyst is the "total metals content" which is defined to be the sum of the platinum or palladium component, the bismuth component, and the rhodium component, calculated on an elemental basis. Good results are ordinarily obtained with the subject catalyst when this parameter is fixed at a value of about 0.15 to about 2.5 wt. %, with best results ordinarily achieved at a metals loading of about 0.3 to about 2 wt. %.
An optional ingredient for the trimetallic catalyst of the present invention is a Friedel-Crafts metal halide component. This ingredient is particularly useful in hydrocarbon conversion embodiments of the present invention, wherein it is preferred that the catalyst utilized has a strong acid or cracking function associated therewith--for example, an embodiment wherein hydrocarbons are to be hydrocracked or isomerized with the catalyst of the present invention. Suitable metal halides of the Friedel-Crafts type include aluminum chloride, aluminum bromide, ferric chloride, ferric bromide, zinc chloride, and the like compounds, with the aluminum halides and particularly aluminum chloride ordinarily yielding best results. Generally, this optional ingredient can be incorporated into the composite of the present invention by any of the conventional methods for adding metallic halides of this type; however, best results are ordinarily obtained when the metallic halide is sublimed onto the surface of the carrier material according to the preferred method disclosed in U.S. Pat. No. 2,999,074. The component can generally be utilized in any amount which is catalytically effective, with a value selected from the range of about 1 to about 100 wt. % of the carrier material generally being preferred.
Regardless of the details of how the components of the catalyst are combined with the porous carrier material, the final catalyst generally will be dried at a temperature of about 200.degree. to about 600.degree. F. for a period of at least about 2 to 24 hours or more, and finally calcined or oxidized at a temperature of about 700.degree. F. to about 1100.degree. F. in an air or oxygen atmosphere for a period of about 0.5 to about 10 hours in order to convert substantially all of the metallic components to the corresponding oxide forms. Because a halogen component is utilized in the catalyst, best results are generally obtained when the halogen content of the catalyst is adjusted during the calcination step by including a halogen, hydrogen halide, or a halogen-containing compound in the air atmosphere utilized. In particular, when the halogen component of the catalyst is combined chloride, it is preferred to use a mole ratio of H.sub.2 O to HCl of about 5:1 to about 100:1 during at least a portion of the calcination step in order to adjust the final chlorine content of the catalyst to a range of about 0.1 to about 3.5 wt. %.
It is an essential feature of the present invention that the resultant oxidized trimetallic catalytic composite is subjected to a substantially water-free reduction step prior to its use in the conversion of hydrocarbons. This step is designed to insure a uniform and finely divided dispersion of the metallic components throughout the carrier material and to selectively reduce substantially all of the platinum or palladium component, the rhodium component, and the bismuth component to the corresponding metals. Preferably, substantially pure and dry hydrogen (i.e., less than 20 vol. ppm. H.sub.2 O) is used as the reducing agent in this step. The reducing agent is contacted with the oxidized catalyst at conditions including a temperature of about 800.degree. F. to about 1200.degree. F., a gas hourly space velocity of about 100 to about 5000 hr..sup..sup.-1, and a period of time of about 0.5 to 10 hours effective to reduce substantially all of the platinum or palladium, rhodium, and bismuth components to the corresponding elemental metallic states. This reduction treatment may be performed in situ as part of a startup sequence if precautions are taken to predry the plant to a substantially water-free state and if substantially water-free hydrogen is used.
The resulting reduced catalytic composite may, in some cases, be beneficially subjected to a presulfiding operation designed to incorporate in the catalytic composite from about 0.01 to about 0.5 wt. % sulfur, calculated on an elemental basis, in the form of the adsorbed sulfide. Preferably, this presulfiding treatment takes place in the presence of hydrogen and a sulfiding reagent which is a suitable sulfur-containing and metallic sulfide-producing compound such as hydrogen sulfide, lower molecular weight mercaptans, organic sulfide, disulfides, etc. Typically, this procedure comprises treating the selectively reduced catalyst with a sulfiding gas such as a mixture of hydrogen and hydrogen sulfide having about 10 moles of hydrogen per mole of hydrogen sulfide at conditions sufficient to effect the desired incorporation of sulfur, generally including a temperature ranging from about 50.degree. F. up to about 1100.degree. F. or more. It is generally a good practice to perform this presulfiding step under substantially water-free conditions.
According to the present invention, a hydrocarbon charge stock and hydrogen are contacted with the previously characterized trimetallic catalyst in a hydrocarbon conversion zone. This contacting may be accomplished by using the catalyst in a fixed bed system, a moving bed system, a fluidized bed system, or in a batch type operation; however, in view of the danger of attrition losses of the valuable catalyst, and of well known operational advantages, it is preferred to use a fixed bed system. In this system, a hydrogen-rich gas and the charge stock are preheated by any suitable heating means to the desired reaction temperature and then are passed into a conversion zone containing a fixed bed of the catalyst type previously characterized. It is, of course, understood that the conversion zone may be one or more separate reactors with suitable means therebetween to insure that the desired conversion temperature is maintained at the entrance to each reactor. It is also important to note that the reactants may be contacted with the catalyst bed in either upward, downward, or radial flow fashion with the latter being preferred. In addition, the reactants may be in the liquid phase, a mixed liquid-vapor phase, or a vapor phase when they contact the catalyst, with best results obtained in the vapor phase.
In the case where the trimetallic catalyst of the present invention is used in a reforming operation, the reforming system will comprise a reforming zone containing a fixed bed or moving bed of the instant trimetallic catalyst. This reforming zone may be one or more separate reactors with suitable heating means therebetween to compensate for the endothermic nature of the reactions that take place in each catalyst bed. The hydrocarbon feed stream that is charged to this reforming system will comprise hydrocarbon fractions containing naphthenes and paraffins that boil within the gasoline range. The preferred charge stocks are those consisting essentially of naphthenes and paraffins, although in some cases aromatics and/or olefins may also be present. This preferred class includes straight run gasolines, natural gasolines, synthetic gasolines, and the like. On the other hand, it is frequently advantageous to charge thermally or catalytically cracked gasolines or higher boiling fractions thereof. Mixtures of straight run and cracked gasolines can also be used to advantage. The gasoline charge stock may be a full boiling gasoline having an initial boiling point of from about 50.degree. F. to about 150.degree. F. and an end boiling point within the range of from about 325.degree. F. to about 425.degree. F., or may be a selected fraction thereof which generally will be a higher boiling fraction commonly referred to as a heavy naphtha--for example, a naphtha boiling in the range of C.sub.7 to 400.degree. F. In some cases, it is also advantageous to charge pure hydrocarbons or mixtures of hydrocarbons that have been extracted from hydrocarbon distillates--for example, straight-chain paraffins--which are to be converted to aromatics. It is preferred that these charge stocks be treated by conventional catalytic pretreatment methods such as hydrorefining, hydrotreating, hydrodesulfurization, etc., to remove substantially all sulfurous, nitrogenous, and water-yielding contaminants therefrom and to saturate any olefins that may be contained therein.
In other hydrocarbon conversion embodiments, the charge stock will be of the conventional type customarily used for the particular kind of hydrocarbon conversion being effected. For example, in a typical isomerization embodiment the charge stock can be a paraffinic stock rich in C.sub.4 to C.sub.8 normal paraffins, or a normal butane-rich stock, or an n-hexane-rich stock, or a mixture of xylene isomers, etc. In a dehydrogenation embodiment, the charge stock can be any of the known dehydrogenatable hydrocarbons such as an aliphatic compound containing 2 to 30 carbon atoms per molecule, a C.sub.4 to C.sub.30 normal paraffin, a C.sub.8 to C.sub.12 alkylaromatic, a naphthene, and the like. In hydrocracking embodiments, the charge stock will be typically a gas oil, heavy cracked cycle oil, etc. In addition, alkylaromatic and naphthenes can be conveniently isomerized by using the catalyst of the present invention. Likewise, pure hydrocarbons or substantially pure hydrocarbons can be converted to more valuable products by using the trimetallic catalyst of the present invention in any of the hydrocarbon conversion processes, known to the art, that use a dual-function catalyst.
In a reforming embodiment, it is generally preferred to utilize the novel trimetallic catalyst composite in a substantially water-free environment. Essential to the achievement of this condition in the reforming zone is the control of the water level present in the charge stock and the hydrogen stream which is being charged. to the zone. Best results are ordinarily obtained when the total amount of water entering the conversion zone from any source is held to a level less than 50 ppm. and preferably less than 20 ppm.; expressed as weight of equivalent water in the charge stock. In general, this can be accomplished by careful control of the water present in the charge stock and in the hydrogen stream. The charge stock can be dried by using any suitable drying means known to the art such as a conventional solid adsorbent having a high selecitivity for water; for instance, sodium or calcium crystalline aluminosilicates, silica gel, activated alumina, molecular sieves, anhydrous calcium sulfate, high surface area sodium, and the like adsorbents. Similarly, the water content of the charge stock may be adjusted by suitable stripping operations in a fractionation column or like device. And in some cases, a combination of adsorbent drying and distillation drying may be used advantageously to effect almost complete removal of water from the charge stock. Preferably, the charge stock is dried to a level corresponding to less than 20 ppm. of H.sub.2 O equivalent. In general, it is preferred to maintain the hydrogen stream entering the hydrocarbon conversion zone at a level of about 10 to about 20 vol. ppm. of water or less. In the case where the water content of the hydrogen stream is above this range, this can be conveniently accomplished by contacting the hydrogen stream with a suitable desiccant such as those mentioned above at conventional drying conditions.
In the reforming embodiment, an effluent stream is withdrawn from the reforming zone and passed through a cooling means to a separation zone, typically maintained at about 25.degree. to 150.degree. F., wherein a hydrogen-rich gas is separated from a high octane liquid product, commonly called an "unstabilized reformate". When a superdry operation is desired, at least a portion of this hydrogen-rich gas is withdrawn from the separating zone and passed through an adsorption zone containing an adsorbent selective for water. The resultant substantially water-free hydrogen stream can then be recycled through suitable compressing means back to the reforming zone. The liquid phase from the separating zone is typically withdrawn and commonly treated in a fractionating system in order to adjust the butane concentration, thereby controlling front end volatility of the resulting reformate.
The conditions utilized in the numerous hydrocarbon conversion embodiments of the present invention are those customarily used in the art for the particular reaction, or combination of reactions, that is to be effected. For instance, alkylaromatic and paraffin isomerization conditions include: a temperature of about 32.degree. F. to about 1000.degree. F. and preferably about 75.degree. F. to about 600.degree. F.; a pressure of atmospheric to about 100 atmospheres; a hydrogen to hydrocarbon mole ratio of about 0.5:1 to about 20:1 and a LHSV (calculated on the basis of equivalent liquid volume of the charge stock contacted with the catalyst per hour divided by the volume of conversion zone containing catalyst) of about 0.2 hr..sup..sup.-1 to 10 hr..sup..sup.-1. Dehydrogenation conditions include: a temperature of about 700 to about 1250.degree. F., a pressure of about 0.1 to about 10 atmospheres, a liquid hourly space velocity of about 1 to 40 hr..sup..sup.-1 and a hydrogen to hydrocarbon mole ratio of about 1:1 to 20:1. Likewise, typically hydrocracking conditions include: a pressure of about 500 psig. to about 3000 psig.; a temperature of about 400.degree. F. to about 900.degree. F.; a LHSV of about 0.1 hr..sup..sup.-1 to about 10 hr..sup..sup.-1 ; and hydrogen circulation rates of about 1000 to 10,000 SCF per barrel of charge.
In the reforming embodiment of the present invention the pressure utilized is selected from the range of about 0 psig. to about 1000 psig., with the preferred pressure being about 50 psig. to about 600 psig. Particularly good results are abtained at low pressure; namely, a pressure of about 50 to 350 psig. In fact, it is a singular advantage of the present invention that it allows stable operation at lower pressure than have heretofore been successfully utilized in so-called "continuous" reforming systems (i.e., reforming for periods of about 15 to about 200 or more barrels of charge per pound of catalyst without regeneration) with all platinum monometallic catalysts. In other words, the trimetallic catalyst of the present invention allows the operation of a continuous reforming system to be conducted at low pressure (i.e., 100 to about 350 psig.) for about the same or better catalyst life before regeneration as has been heretofore realized with conventional monometallic catalysts at higher pressure (i.e., 400 to 600 psig.). On the other hand, the stability feature of the present invention enables reforming operation conducted at pressures of 400 to 600 psig. to achieve substantially increased catalyst life before regeneration.
Similarly, the temperature required for reforming is generally lower than that required for a similar reforming operation using a high quality catalyst of the prior art. This significant and desirable feature of the present invention is a consequence of the selectivity of the trimetallic catalyst of the present invention for the octane-upgrading reactions that are preferably induced in a typical reforming operation. Hence the present invention requires a temperature in the range of from about 800.degree. F. to about 1100.degree. F. and preferably about 900.degree. F. to about 1050.degree. F. As is well known to those skilled in the continuous reforming art, the initial selection of the temperature within this broad range is made primarily as a function of the desired octane of the product reformate considering the characteristics of the charge stock and of the catalyst. Ordinarily, the temperature then is thereafter slowly increased during the run to compensate for the inevitable deactivation that occurs to provide a constant octane product. Therefore, it is a feature of the present invention that the rate at which the temperature is increased in order to maintain a constant octane product, is substantially lower for the catalyst of the present invention than for a high quality reforming catalyst which is manufactured in exactly the same manner as the catalyst of the present invention except for the inclusion of the bismuth and rhodium components. Moreover, for the catalyst of the present invention, the C.sub.5 + yield loss for a given temperature increase is substantially lower than for a high quality reforming catalyst of the prior art. In addition, hydrogen production is substantially higher.
The reforming embodiment of the present invention also typically utilizes sufficient hydrogen to provide an amount of about 1 to 20 moles of hydrogen per mole of hydrocarbon entering the reforming zone, with excellent results being obtained when about 5 to about 10 moles of hydrogen are used per mole of hydrocarbon. Likewise, the liquid hourly space velocity, (LHSV), used in reforming is selected from the range of about 0.1 to about 10 hr..sup..sup.-1, with a value in the range of about 1 to about 5 hr..sup..sup.-1 being preferred. In fact, it is a feature of the present invention that it allows operations to be conducted at higher LHSV than normally can be stably achieved in a continuous reforming process with a high quality reforming catalyst of the prior art. This last feature is of immense economic significance because it allows a continuous reforming process to operate at the same throughput level with less catalyst inventory than that heretofore used with conventional reforming catalysts at no sacrifice in catalyst life before regeneration.
The following working examples are given to illustrate further the preparation of the trimetallic catalytic composite of the present invention and the use thereof in the conversion of hydrocarbons. It is understood that the examples are intended to be illustrative rather than restrictive.

EXAMPLE I
This example demonstrates a particularly good method of preparing the trimetallic catalytic composite of the present invention.
An alumina carrier material comprising 1/16 inch spheres is prepared by: forming an aluminum hydroxyl chloride sol by dissolving substantially pure aluminum pellets in hydrochloric acid, adding hexamethylenetetramine to the resulting alumina sol, gelling the resulting solution by dropping it into an oil bath to form spherical particles of an aluminum-containing hydrogel, aging and washing the resulting particles, and finally drying and calcining the aged and washed particles to form spherical particles of gamma-alumina containing about 0.3 wt. % combined chloride. Additional details as to this method of preparing the preferred gamma-alumina carrier material are given in the teachings of U.S. Pat. No. 2,620,314.
An aqueous impregnation solution containing chloroplatinic acid, rhodium trichloride hydrate, bismuth trichloride, and hydrogen chloride is then prepared. The alumina carrier material is thereafter admixed with the impregnation solution. The amount of regents contained in this impregnation solution is calculated to result in a final composite containing, on an elemental basis, 0.375 wt. % platinum, 0.25 wt. % bismuth, and 0.25 wt. % rhodium. In order to insure uniform dispersion of the metallic components throughout the carrier material, the amount of hydrochloric acid used is about 3 wt. % of the alumina particles. This impregnation step is performed by adding the carrier material particles to the impregnation mixture with constant agitation. In addition, the volume of the solution is approximately the same as the void volume of the carrier material particles. The impregnation mixture is maintained in contact with the carrier material particles for a period of about 1/2 hour at a temperature of about 70.degree. F. Thereafter, the temperature of the impregnation mixture is raised to about 225.degree. F. and the excess solution evaporated in a period of about 1 hour. The resulting dried particles are then subjected to a calcination or oxidation treatment in an air atmosphere at a temperature of about 975.degree. F. for about 1 hour. This oxidation step is designed to convert substantially all of the metallic ingredients to the corresponding oxide forms. The calcined spheres are then contacted with an air stream containing H.sub.2 O and HCl in a mole ratio of about 30:1 for about 4 hours at 975.degree. F. in order to adjust the halogen content of the catalyst particles to a value of about 1 wt. %.
The resulting catalyst particles were analyzed and found to contain, on an elemental basis, about 0.375 wt. % platinum, about 0.25 wt. % rhodium, about 0.25 wt. % bismuth, and about 1 wt. % combined chloride. For this catalyst, the atomic ratio of rhodium to platinum is 1.26:1 and the atomic ratio of bismuth to platinum is 0.622:1.
Thereafter, the catalyst particles are subjected to a dry reduction step, designed to reduce the platinum, rhodium, and bismuth components to the corresponding elemental metallic states by contacting them for 1 hour with a substantially pure hydrogen stream containing less than 5 vol. ppm. H.sub.2 O at a temperature of about 1050.degree. F., a pressure slightly above atmospheric, and a flow rate of the hydrogen stream through the catalyst particles corresponding to a gas hourly space velocity of about 720 hr..sup..sup.-1.
EXAMPLE II
A portion of the Example trimetallic catalyst particles produced by the method described in Examplle I are loaded into a scale model of a continuous, fixed bed reforming plant of conventional design. In this plant, a heavy Kuwait naphtha and hydrogen are continuously contacted at reforming conditions: a liquid hourly space velocity of 1.5 hr..sup..sup.-1 ; a pressure of 100 psig.; a hydrogen to hydrocarbon mole ratio of 5:1, and a temperature sufficient to continuously produce a C.sub.5 + reformate of 102 F-1 clear. It is to be noted that these are exceptionally severe conditions.
The heavy Kuwait naphtha has a API gravity at 60.degree. F. of 60.4, an initial boiling point of 184.degree. F., a 50% boiling point of 256.degree. F., and an end boiling point of 360.degree. F. In addition, it contains about 8 vol. % aromatics, 71 vol. % paraffins 21 vol. % naphthenes, 0.5 wt. % parts per million sulfur, and 5 to 8 wt. parts per million water. The F-1 clear octane number of the raw stock is 40.0.
The fixed bed reforming plant is made up of a reactor containing the trimetallic catalyst, a hydrogen separation zone, a debutanizer column, and suitable heating, pumping, cooling, and controlling means. In this plant, a hydrogen recycle stream and the charge stock are commingled and heated to the desired temperature. The resultant mixture is then passed downflow into a reactor containing the trimetallic catalyst as a fixed bed. An effluent stream is then withdrawn from the bottom of the reactor, cooled to about 55.degree. F. and passed to a separating zone wherein a hydrogen-rich gaseous phase separates from a liquid hydrocarbon phase. A portion of the gaseous phase is continuously passed through a high surface area sodium scrubber and the resulting water-free hydrogen stream recycled to the reactor in order to supply hydrogen thereto and the excess hydrogen over that needed for plant pressure is recovered as excess separator gas. The liquid hydrocarbon phase from the hydrogen separating zone is withdrawn therefrom and passed to a debutanizer column of conventional design wherein light ends are taken overhead as debutanizer gas and C.sub.5 + reformate stream recovered as bottoms.
The test run is continued for a catalyst life of about 20 barrels of charge per pound of catalyst utilized, and it is determined that the activity, selectivity, and stability of the present trimetallic catalyst are vastly superior to those observed in a similar type test with a conventional commercial reforming catalyst. More specifically, the results obtained from the subject catalyst are superior to the platinum metal-containing catalyst of the prior art in the areas of hydrogen production, C.sub.5 + yield at octane, average rate of temperature increase necessary to maintain octane, and C.sub.5 + yield decline rate.
It is intended to cover by the following claims all changes and modifications of the above disclosure of the present invention which would be self-evident to a man of ordinary skill in the catalyst formulation art of the hydrocarbon conversion art.

Number	Name	Date
3651163	Radford et al.	Mar 1972
3655747	Sennewald et al.	Jun 1972
3827972	Kominami et al.	Aug 1974
3839225	Acres	Oct 1974

	Number	Date	Country
Parent	436305	Jan 1974
Parent	233819	Mar 1972

Hydrocarbon conversion with a multimetallic catalytic composite

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Continuation in Parts (2)