Catalytic process for the conversion of hydrocarbons

BACKGROUND OF THE INVENTION
The present invention is directed toward a novel hydrocarbon conversion process, especially for effecting the dehydrocyclization of aliphatic hydrocarbons to aromatics. More particularly, the novel process enables the conversion of C.sub.6 -plus paraffins to their corresponding aromatics with a high degree of selectivity thereby enabling the facile production of large quantities of aromatics.
In the past, it has become the practice to effect conversion of aliphatic hydrocarbons to aromatics by means of the well-known catalytic reforming process. In catalytic reforming, a hydrocarbonaceous feedstock, typically a petroleum naphtha fraction, is contacted with a Group VIII-containing catalytic composite to produce a product reformate of increased aromatics content. The naphtha fraction is typically a full boiling range fraction having an initial boiling point of from about 10.degree.-38.degree. C. and an end boiling point of from about 107.degree.-218.degree. C. Such a full boiling range naphtha contains significant amounts of C.sub.6 -plus paraffinic hydrocarbons and C.sub.6 -plus naphthenic hydrocarbons. As is well known, these paraffinic and naphthenic hydrocarbons are converted to aromatics by means of multifarious reaction mechanisms. These mechanisms include dehydrogenation, dehydrocyclization, and isomerization followed by dehydrogenation. Accordingly, naphthenic hydrocarbons are converted to aromatics by dehydrogenation. Paraffinic hydrocarbons may be converted to the desired aromatics by dehydrocyclization and may also undergo isomerization. Accordingly then, it is apparent that the number of reactions taking place in a catalytic reforming zone are numerous and the typical reforming catalyst must be capable of effecting numerous reactions to be considered usable in a commercially feasible reaction system.
Because of the complexity and number of reaction mechanisms ongoing in catalytic reforming, it has become a recent practice to develop highly specific catalysts tailored to convert only specific reaction species to aromatics. Such catalysts offer advantages over the typical reforming catalyst which must be capable of taking part in numerous reaction mechanisms. Ongoing work has been directed toward producing a catalyst for the conversion of paraffinic hydrocarbons, particularly having six carbon atoms or more, to the corresponding aromatic hydrocarbon. Such a catalyst can be expected to be much more specific resulting in less undesirable side reactions such as hydrocracking. As can be appreciated by those of ordinary skill in the art, increased production of aromatics is desirable. The increased aromatic content of gasolines, a result of lead phase down, as well as demands in the petrochemical industry make C.sub.6 -C.sub.8 aromatics highly desirable products. Accordingly, it would be most advantageous to have a process and a catalytic composition which is highly selective for the conversion of less valuable C.sub.6 -plus paraffins to the more valuable C.sub.6 -plus aromatics.
OBJECTS AND EMBODIMENTS
It is, therefore, a principal object of the present invention to provide a process utilizing a novel catalytic composition for the conversion of hydrocarbons. A more specific objective is to provide a process for the conversion of C.sub.6 -plus paraffinic hydrocarbons, especially C.sub.6 -C.sub.8 paraffinic hydrocarbons, to their corresponding aromatics.
Accordingly, a broad embodiment of the present invention is directed toward a dehydrocyclization process characterized in that it comprises contacting at catalytic dehydrocyclization conditions a hydrocarbon charge stock with a catalytic composite comprising a nonacidic L-zeolite, a catalytically effective amount of a Group VIII metal component, and sufficient surface-deposited alkali metal to provide a surface-deposited alkali metal index of from about 40 to about 500, where the catalytic composite is prepared without subjecting the L-zeolite to a solution having a pH of greater than 9 and without appreciable loss of SiO.sub.2 from the L-zeolite.
These as well as other objects and embodiments will become evident from the following, more detailed description of the present invention.
INFORMATION DISCLOSURE
Aluminosilicates containing alkali metals are well known in the art. For example, U.S. Pat. No. 3,013,986, issued Dec. 19, 1968, discloses an alkali metal loaded L-zeolite. In particular, this reference indicates that the potassium or the potassium/sodium form of the L-zeolite are the preferred starting materials for the alkali metal-loaded L-zeolite. The reference teaches that a dehydrated molecular sieve may be contacted with alkali metal vapors to produce an alkali metal-loaded molecular sieve wherein the alkali metal is contained within the interior of the zeolitic molecular sieve. The reference, however, does not disclose a nonacidic zeolite having composited therewith catalytically effective amounts of Group VIII metal component and surface-deposited alkali metal. Moreover, the reference does not disclose that such a composition would have any use as a hydrocarbon conversion catalyst.
U.S. Pat. No. 3,376,215, issued Apr. 2, 1968, discloses a hydrocarbon conversion catalyst comprising a cocatalytic solid support containing a Group VIII metal which support comprises (1) an adsorbent refractory inorganic oxide and (2) a mordenite structure zeolite having deposited thereon about 10 to about 1000 ppm by weight, based on zeolite, of a metal selected from the class of alkali metals, alkaline earth metals, and mixtures thereof. This reference teaches that the support comprising a mordenite form zeolite and a refractory oxide be cocatalytic. By way of contrast, an essential feature of the present invention is use of a nonacidic zeolite. In this nonacidic form, the zeolite of the present invention is not catalytic. Rather, the nonacidic zeolite acts to modify the catalytic Group VIII metal of the present invention. Accordingly, this reference does not disclose the novel catalyst of the present invention.
U.S. Pat. No. 3,755,486, issued Aug. 28, 1973, discloses a process for dehydrocyclizing C.sub.6 -C.sub.10 hydrocarbons having at least a C.sub.6 backbone using an Li, Na, or K zeolite X or Y or faujasite impregnated with 0.3 to 1.4% platinum. This reference, however, fails to disclose the advantages to be derived by utilizing a catalytic composite comprising a nonacidic zeolite having surface-deposited alkali metal. Likewise, U.S. Pat. No. 3,819,507, issued June 25, 1974, and U.S. Pat. No. 3,832,414, issued Aug. 27, 1974, while disclosing processes similar to that of U.S. Pat. No. 3,755,486, both fail to teach the use and advantages to be derived by such use of a nonacidic zeolite composited with platinum and surface-deposited alkali metal.
U.S. Pat. No. 4,140,320, issued Aug. 1, 1978, discloses a process for dehydrocyclizing aliphatic hydrocarbons utilizing a type L-zeolite having exchangeable cations of which at least 90% are alkali metal ions selected from the group consisting of ions of sodium, lithium, potassium, rubidium and cesium and containing at least one metal selected from the group which consists of metals of Group VIII, tin and germanium. This reference fails to disclose the catalytic composite of the present invention in that the alkali metal ions of the catalyst of this reference are all associated with ion exchange sites on the L-zeolite. There is no disclosure of an L-zeolite having surface-deposited alkali metal. U.S. Pat. No. 4,417,083, issued Nov. 22, 1983, discloses a process for dehydrocyclization utilizing a substantially nonacidic zeolite having a pore diameter larger than 6.5 angstroms and containing at least one metal selected from the group consisting of platinum, rhenium, iridium, tin, and germanium. Additionally, the catalyst contains sulfur and alkaline cations. However, in this reference, there is no disclosure of surface-deposited alkali metal. U.S. Pat. No. 4,416,806, issued Nov. 22, 1983, discloses yet another paraffin dehydrocyclization catalyst comprising platinum, rhenium as a carbonyl, and sulfur on a zeolitic crystalline aluminosilicate compensated in more than 90% by alkaline cations and having a pore diameter of more than 6.5 angstroms. This reference too, fails to disclose a catalytic composition for dehydrocyclization having surface-deposited alkali metal.
U.S. Pat. No. 4,430,200, issued Feb. 7, 1984, discloses a hydrocarbon conversion catalyst comprising a high silica zeolite such as mordenite or zeolite Y which has been base exchanged with an alkali metal. This reference too, however, fails to disclose a catalyst with surface-deposited alkali metal. Moreover, the reference merely discloses the use of the prior art catalyst in a cracking process and not a dehydrocyclization process.
U.S. Pat. No. 4,448,891, issued May 15, 1984, discloses a dehydrocyclization catalyst comprising an L-zeolite which has been soaked in an alkali solution having a pH of at least 11 for a time and at a temperature effective to increase the period of time over which the catalytic activity of the catalyst is maintained. Additionally, the catalyst contains a Group VIII metal. However, in the reference, the alkali soak is taught as modifying the silica content of the L-zeolite by reducing the SiO.sub.2 content and altering the structure of the zeolite. After the alkali soak, the reference indicates that the L-zeolite is washed to remove excess ions. Accordingly, the catalyst of this reference does not have deposited thereon surface-deposited alkali metal. It, therefore, does not disclose the catalyst of the instant invention.
In summary then, the art has not recognized a dehydrocyclization process characterized in that it comprises contacting at catalytic dehydrocyclization conditions a hydrocarbon charge stock with a catalytic composite comprising a nonacidic L-zeolite, a catalytically effective amount of a Group VIII metal component, and sufficient surface-deposited alkali metal to provide a surface-deposited alkali metal index of from about 40 to about 500, where the catalytic composite is prepared without subjecting the L-zeolite to a solution having a pH of greater than 9 and without appreciable loss of SiO.sub.2 from the L-zeolite. Moreover, the art has not recognized the attendant advantages to be derived from such a novel catalyst and use thereof.
DETAILED DESCRIPTION OF THE INVENTION
To reiterate briefly, the present invention relates to a dehydrocyclization process characterized in that it comprises contacting at catalytic dehydrocyclization conditions a hydrocarbon charge stock with a catalytic composite comprising a nonacidic L-zeolite, a catalytically effective amount of a Group VIII metal component, and sufficient surface-deposited alkali metal to provide a surface-deposited alkali metal index of from about 40 to about 500. Specifically, the catalytic composition is prepared without subjecting the L-zeolite to a solution pH of greater than 9 and without appreciable loss of SiO.sub.2 from the zeolite. Moreover, the process of the invention has particular utility as a catalyst for the dehydrocyclization of C.sub.6 -plus paraffins, especially C.sub.6 -C.sub.10 paraffins.
As heretofore indicated, it is an essential feature of the catalyst of the present invention that it comprise a nonacidic L-zeolite. By "nonacidic zeolite", it is to be understood that it is meant that the zeolite has substantially all of its cationic sites of exchange occupied by nonhydrogen cationic species. Preferably, such cationic species will comprise the alkali metal cations although other cationic species may be present. Irrespective of the actual cationic species present in the sites of exchange, the nonacidic zeolite in the present invention has substantially all of the cationic sites occupied by nonhydrogen cations, thereby rendering the zeolite substantially fully cationic exchanged. Many means are well known in the art for arriving at a substantially fully cationic exchanged zeolite and thus they need not be elaborated herein. The nonacidic zeolite of the present invention acts to modify the catalytic Group VIII metal and is substantially inert in the reaction. It is believed that the nonacidic zeolite of the present invention is noncatalytic and hence the requirement that it be nonacidic.
The especially preferred type of nonacidic zeolite of the present invention is L-zeolite. It is required that the cationic exchangeable sites of the L-zeolite be fully cationic exchanged with nonhydrogen cationic species. As also indicated above, typically the cations occupying the cationic exchangeable sites will comprise one or more of the alkali metals including lithium, sodium, potassium, rubidium, and cesium. An especially preferred nonacidic zeolite for application in the present invention is the potassium form of L-zeolite. It should also be understood, however, that the nonacidic L-zeolite of the invention may contain more than one type of the alkali metal cation at the cationic exchangeable sites, for example, sodium and potassium. As will be explained more fully hereinafter, this can occur as the result of competitive cationic exchanges which may take place during the deposition of the surface-deposited alkali metal. It is contemplated that the nonacidic L-zeolite may be intimately associated with a support matrix, however, the preferred formulation of the catalytic composite of the instant invention does not contain a support matrix. Thus, the catalytic composite comprises a non-matrix support nonacidic L-zeolite.
As is well known in the art, use of a support matrix enhances the physical strength of the catalyst. Additionally, use of a support matrix allows formation of shapes suitable for use in catalytic conversion processes. For example, the nonacidic zeolite of the present invention may be bound in the support matrix such that the final shape of the catalytic composite is a sphere. The use of spherical shaped catalyst is, of course, well known to be advantageous in various applications. In particular, when the catalyst of the instant invention is employed within a continuously moving bed hydrocarbon conversion process, a spherical shape enhances the ability of the catalyst to move easily through the reaction and regeneration zones. Of course, other shapes may be employed where advantageous. Accordingly, the catalytic composite may be formed into extrudates, saddles, etc.
The support matrix may comprise any support matrix typically utilized to bind zeolitic-containing catalytic composites. Such support matrices are well known in the art and include clays, bauxite, refractory inorganic oxides such as alumina, zirconium dioxide, hafnium oxide, beryllium oxide, vanadium oxide, cesium oxide, chromium oxide, zinc oxide, magnesia, thoria, boria, silica-magnesia, chromia-alumina, alumina-boria, etc. A preferred support matrix comprises silica, and an especially preferred support matrix comprises alumina. It is further preferred that the support matrix be substantially inert to the reactants to be converted by the composite as well as the other constituents of the composite. To this end, it is preferred that the support matrix be nonacidic to avoid promotion of undesirable side reactions. Such nonacidity may be induced by the presence of alkali metals such as those comprising the surface-deposited alkali metal.
If a support matrix is used to bind the nonacidic L-zeolite, the procedure for binding may be by any method known in the art. Such methods include pilling, extruding, granulating, marumarizing, etc. A particularly preferred method is the so-called oil-drop method.
Typically, in binding a zeolite in a support matrix by means of the oil-drop method, powdered zeolite is admixed with a sol comprising the desired support matrix or precursors thereof, and a gelling agent. Droplets of the resulting admixture are dispersed as spherical droplets in a suspending medium, typically oil. The gelling agent thereafter begins to cause gelation of the sol as a result of the change in the sol pH. The resulting gelled support matrix has bound therein the zeolite. The suspending medium helps maintain the spherical shape of the droplets. Useable suspending mediums include Nujol, kerosene, selected fractions of gas oil, etc. Many gelling agents are known in the art and include both acids and bases. Hexamethylenetetramine is only one such known gelling agent. The hexamethylenetetramine slowly decomposes to ammonia upon heating. This results in a gradual pH change and as a result, a gradual gelation.
Regardless of the exact method of binding the nonacidic L-zeolite in the support matrix, sufficient nonacidic L-zeolite may be used to result in a catalytic composite comprising from about 25 to about 75 wt.% nonacidic L-zeolite based on the weight of the zeolite and support matrix. The exact amount of nonacidic L-zeolite advantageously included in the catalytic composite will be a function of the support matrix and the specific application of the catalytic composite. A catalytic composite comprising about 50 to 75 wt.% potassium form of L-zeolite bound in alumina is advantageously used in the dehydrocyclization of C.sub.6 -C.sub.8 nonaromatic hydrocarbons.
A further essential feature of the catalyst of the present invention is the presence of catalytically effective amounts of a Group VIII metal component, including catalytically effective amounts of nickel component, rhodium component, palladium component, iridium component, platinum component, or mixtures thereof. Especially preferred among the Group VIII metal components is a platinum component. The Group VIII metal component may be composited with the other constituents of the catalytic composite by any suitable means known in the art. For example, a platinum component may be impregnated by means of an appropriate solution such as a dilute chloroplatinic acid solution. Alternatively, the Group VIII metal component may be composited by means of ion exchange in which case, some of the cationic exchange sites of the nonacidic zeolite may contain Group VIII metal cations. After ion exchange, the Group VIII metal may be subject to a low temperature oxidation prior to any reduction step. The Group VIII metal component may be composited with the other constituents either prior to or subsequent to the deposition of the hereinafter described surface-deposited alkali metal. Additionally, the Group VIII metal may be composited with the nonacidic zeolite and thereafter, the nonacidic zeolite containing Group VIII metal may be bound with the support matrix.
Irrespective of the exact method of compositing the Group VIII metal component into the catalytic composite, any catalytically effective amount of Group VIII metal component may be employed. The optimum Group VIII metal component content will depend generally on which Group VIII metal component is utilized in the catalyst of the invention. However, generally from about 0.01 to about 5.0 wt.% of the Group VIII metal component based on the weight of the nonacidic L-zeolite, Group VIII metal component and surface-deposited alkali metal may be advantageously utilized.
It is believed that best results are achieved when the Group VIII metal is substantially all deposited on the nonacidic zeolite. It is also advantageous to have the Group VIII metal component highly dispersed. The Group VIII metal component is most effective in a reduced state. Any suitable means may be employed for reducing the Group VIII metal component and many are well known in the art. For example, after compositing, the Group VIII metal component may be subjected to contact with a suitable reducing agent, such as hydrogen, at an elevated temperature for a period of time.
In addition to comprising a Group VIII metal component, it is contemplated in the present invention that the catalyst thereof may contain other metal components well known to have catalyst modifying properties. Such metal components include rhenium, tin, cobalt, indium, gallium, lead, zinc, uranium, thallium, dysprosium, germanium, etc. Incorporation of such metal components have proven beneficial in catalytic reforming as promoters and/or extenders. Accordingly, it is within the scope of the present invention that catalytically effective amounts of such modifiers may be beneficially incorporated into the catalyst of the present invention improving its performance.
Irrespective of the particular Group VIII metal component or catalytic modifiers composited in the catalyst of the invention, the catalyst of the present invention also comprises sufficient surface-deposited alkali metal to provide a surface-deposited alkali metal index of at least 10 and preferably from about 40 to about 500. It is to be understood that by "surface-deposited alkali metal", it is meant that the alkali metal component is not associated with a cationic exchangeable site, but rather is excess alkali metal component above that amount required to occupy substantially all of the cationic exchangeable sites. It is to be further understood that the surface-deposited alkali metal index is indicative of the amount of such surface-deposited alkali metal. As used herein, the term "surface-deposited alkali metal index" is defined as 10.sup.4 multiplied by the moles per liter of soluble alkali metal yielded by the weight of catalytic composite comprising 0.5 g of nonacidic zeolite placed in 10 cc of deionized water as measured at 25.degree. C. by an electrode sensitive to said alkali metal.
Any of the alkali metals may be used as the surface-deposited alkali-metal including lithium, sodium, potassium, rubidium, cesium, and mixtures thereof. Potassium on the potassium form of L-zeolite is especially preferred.
It should be understood that the surface-deposited alkali metal need not necessarily be the same alkali metal as the cations occupying the cationic exchangeable sites of the nonacidic L-zeolite. Hence, the surface-deposited alkali metal may, for example, comprise rubidium while the nonacidic zeolite may comprise the potassium form of L-zeolite. Likewise, the surface-deposited alkali metal may comprise more than one alkali metal. Accordingly, the surface-deposited alkali metal may, for example, comprise potassium and cesium on the potassium form of L-zeolite.
The surface-deposited alkali metal may be composited with the catalyst of the present invention by any suitable technique. Standard impregnation techniques may be employed utilizing an aqueous solution of an alkali metal salt. Either basic or neutral salts may be used. For example, when surface-depositing potassium on a catalyst comprising the potassium form of L-zeolite, the impregnation solution may comprise a basic salt of potassium such as KHCO.sub.3, K.sub.2 CO.sub.3, KOH, etc. Alternatively, a solution comprising neutral potassium salt such as KCl may be used.
As indicated, a basic alkali metal salt solution may be used to surface-deposit the alkali metal. However, it is a requirement of the present invention that the basicity of such an alkali metal salt solution not be so strong as to modify the zeolite structure. Preferably, the catalyst composite is prepared without subjecting the L-zeolite to a solution having a pH greater than 9. At pH values exceeding 9, silica has tendency to solubilize, thus lowering the SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio of the zeolite as SiO.sub.2 is lost from the zeolite. Concomitant with the silica loss is a reduction of the purity of the L-zeolite as measured by X-ray diffraction analysis. Any appreciable loss of SiO.sub.2 from the L-zeolite and/or loss of zeolite purity introduces uncertainty in the surface deposited alkali metal index measurement.
Therefore, another feature of the present invention is that the catalytic composite be prepared without appreciable loss of SiO.sub.2 from the L-zeolite. What is meant by the term "appreciable" is a silica loss of greater than 0.05 wt.% of SiO.sub.2 based on the weight of the L-zeolite, Group VIII metal component, and surface-deposited alkali metal.
Also associated with silica removal is an expansion in the a.sub.o lattice dimension as measured by X-ray diffraction analysis. Because of the requirement of not contacting the L-zeolite with solutions having a pH greater than 9, catalysts prepared in accordance with the instant invention do not exhibit either the lattice expansion or a decrease in the SiO.sub.2 /Al.sub.2 O.sub.3 molar ratio.
It should further be noted that when it is desired to have a surface-deposited alkali metal different than the alkali metal cation associated with the cation exchangeable sites of the nonacidic L-zeolite, some amount of competitive ion exchange may take place during impregnation. For example, when surface-depositing rubidium on the potassium form of L-zeolite, a competitive ionic exchange may take place wherein some of the rubidium from the impregnation solution replaces some of the potassium on the cationic exchangeable sites of the nonacidic L-zeolite. In turn, this displaced potassium will be surface-deposited on the zeolite along with the balance of the rubidium. The net result is that the cations at the cationic exchangeable sites will comprise rubidium and potassium ions while the surface-deposited alkali metal will comprise rubidium and potassium. A catalyst having such a distribution is within the scope of the present invention, but may not give the best results. There are, however, techniques well known in the art of catalyst preparation to minimize the problem of competitive exchange and as a consequence, further elaboration thereof for one of ordinary skill in the art is unnecessary.
As heretofore indicated, the catalytic composite of the present invention has particular utility as a hydrocarbon conversion catalyst. Accordingly, a hydrocarbon charge stock is contacted at hydrocarbon conversion conditions with the catalytic composite of the present invention. A wide range of hydrocarbon conversion conditions may be employed and the exact conditions will depend upon the particular charge stock and reaction to be effected. Generally, these conditions include a temperature of about 260.degree.-815.degree. C., a pressure of from atmospheric to about 100 atmospheres, a liquid hourly space velocity (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 to 15 hr.sup.-1. Furthermore, hydrocarbon conversion conditions may include the presence of a diluent such as hydrogen. When such is the case, the hydrogen to hydrocarbon mole ratio may be from about 0.5:1 to about 30:1.
As heretofore indicated, the instant invention involves the process of converting a hydrocarbon charge stock at catalytic dehydrocyclization conditions. In particular, the preferred hydrocarbon charge stock comprises C.sub.6 -C.sub.8 nonaromatic hydrocarbons. Accordingly, the present invention involves contacting a hydrocarbon charge stock comprising C.sub.6 -C.sub.8 nonaromatic hydrocarbons with the catalyst described hereinabove at dehydrocyclization conditions. Dehydrocyclization conditions include a pressure of from about 0 to about 1000 psig, with the preferred pressure being from about 25 to about 600 psig, a temperature of from about 427.degree.-650.degree. C., and a liquid hourly space velocity of from about 0.1 to about 10 hr.sup.-1. Preferably, hydrogen may be employed as a diluent. When present, hydrogen may be circulated at a rate of from about 1 to about 10 moles of hydrogen per mole of charge stock hydrocarbon.
In accordance with the present invention, a hydrocarbon charge stock is contacted with the 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. The hydrocarbon charge stock and, if desired, a hydrogen-rich gas as diluent are typically preheated by any suitable heating means to the desired reaction temperature and then are passed into a conversion zone containing the catalyst of the invention. It is, of course, understood that the conversion zone may be one or more separate reactors with suitable means therebetween to ensure that the desired conversion temperature is maintained at the entrance to each reactor. It is also important to know 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. Best results are obtained when the reactants are in the vapor phase.
As indicated heretofore, the catalyst may be utilized within the reaction zone as a fixed-bed system, a moving-bed system, a fluidized-bed system, or in a batch-type operation; however, in view of the operational advantages well recognized in the art, it is preferred to utilize the catalyst of the present invention in a moving-bed system. In such a system, the reaction zone may be one or more separate reactors with heating means therebetween to compensate for the endothermic nature of the dehydrocyclization reaction that takes place in each catalyst bed. The hydrocarbon feedstream, preferably comprising C.sub.6 -C.sub.8 nonaromatic hydrocarbons, is charged to the reaction zone as a continuous moving bed. Therein it is contacted with the hydrocarbon charge stock to effect the dehydrocyclization thereof.
After contact with the catalyst, the hydrocarbon charge stock having undergone dehydrocyclization is withdrawn as an effluent stream from the reaction zone and passed through a cooling means to a separation zone. In the separation zone, the effluent may be separated into various constituents depending upon the desired products. When hydrogen is utilized as a diluent in the reaction zone, the separation zone will typically comprise a vapor-liquid equilibrium separation zone and a fractionation zone. A hydrogen-rich gas is separated from a high octane liquid product containing aromatics generated within the dehydrocyclization zone. After separation, at least a portion of the hydrogen-rich gas may be recycled back to the reaction zone as diluent. The balance of the hydrogen-rich gas may be recovered for use elsewhere. The high octane liquid product comprising aromatics may then be passed to a fractionation zone to separate aromatics from the unconverted constituents of the charge stock. These unconverted constituents may then be passed back to the reaction zone for processing or to other processes for utilization elsewhere.
A wide range of hydrocarbon charge stocks may be employed in the process of the present invention. The exact charge stock utilized will, of course, depend on the precise use of the catalyst. Typically, hydrocarbon charge stocks which may be used in the present invention will contain naphthenes and paraffins, although in some cases, aromatics and olefins may be present. Accordingly, the class of charge stocks which may be utilized includes straight-run naphthas, natural naphthas, synthetic naphthas, and the like. Alternatively, straight-run and cracked naphthas may also be used to advantage. The naphtha charge stock may be a full-boiling range naphtha having an initial boiling point of from about 10.degree.-66.degree. C. and an end boiling point within the range of from about 163.degree.-218.degree. C., or may be a selected fraction thereof. It is preferred that the charge stocks employed in the present invention be treated by conventional catalytic pretreatment methods such as hydrorefining, hydrotreating, hydrodesulfurization, etc., to remove substantially all sulfurous, nitrogenous, and water-yielding contaminants therefrom.
It is preferred that the charge stock of the instant invention substantially comprise paraffins. This, of course, is a result of the fact that the purpose of a dehydrocyclization process is to convert paraffins to aromatics. Because of the value of C.sub.6 -C.sub.8 aromatics, it is additionally preferred that the hydrocarbon charge stock comprise C.sub.6 -C.sub.8 paraffins. However, notwithstanding this preference, the hydrocarbon charge stock may comprise naphthenes, aromatics, and olefins in addition to C.sub.6 -C.sub.8 paraffins.
In order to more fully demonstrate the attendant advantages arising from the present invention, the following examples are set forth. It is to be understood that the following is by way of example only and is not intended as an undue limitation on the otherwise broad scope of the present invention.
It should be understood that there are three parameters useful in evaluating hydrocarbon conversion process and catalyst performance, and in particular in evaluating and comparing dehydrocyclization catalysts. The first is "activity" which is a measure of the catalyst's ability to convert reactants at a specified set of reaction conditions. The second catalyst performance criteria is "selectivity" which is an indication of the catalyst's ability to produce a high yield of the desired product. The third parameter is "stability" which is a measure of the catalyst's ability to maintain its activity and selectivity over time. In the appended examples, the criteria which will be of interest is catalyst selectivity. For purposes of the following, the catalyst of the invention is exemplified as a dehydrocyclization catalyst and the measure of catalyst selectivity is the conversion of the paraffin reactants to aromatics.

BRIEF DESCRIPTION OF THE DRAWING
The drawing graphically illustrates the clear dependency of the aromatics produced, shown as selectivity to aromatics in weight percent, as a function of the measured surface-deposited alkali metal index of the catalyst used. Process Runs A and D, both of the instant invention, yield the highest selectivity to aromatics.

EXAMPLE I
A first catalyst was made in accordance with the invention. Fifty grams of potassium form L-zeolite having an average crystallite size of 275 angstroms were slurried in a solution of 12.8 grams of potassium bicarbonate and 100 cc of deionized water. The potassium/zeolite slurry was evaporated to dryness and then calcined in air at 480.degree. C. for 3 hours. The resulting potassium-impregnated zeolite was then subjected to an ion exchange step in order to composite platinum thereon. This was effected by placing the potassium-impregnated zeolite into 200 cc of a 0.020M. Pt(NH.sub.3).sub.4 Cl.sub.2 /0.90M. KCl solution. After three days at 25.degree. C., the potassium-impregnated, platinum-containing zeolite was filtered from the ion exchange solution and rinsed with 1200 cc of deionized H.sub.2 O. The resulting catalyst was then calcined and reduced at 350.degree. C. The resulting catalyst contained about 0.7 wt.% of platinum and had a surface deposited alkali metal index of about 61. This first catalyst made in accordance with the invention was tested in Run A as described below in Example V.
EXAMPLE II
A second catalyst was prepared by the following method. Fifty grams of potassium form L-zeolite already containing surface-deposited alkali metal was subjected to an ion-exchange step to deposit platinum thereon. The ion exchange step was effected substantially as before utilizing an ion exchange solution comprising Pt(NH.sub.3).sub.4 Cl.sub.2 with KCl. The ion exchanged platinum- and surface-deposited potassium-containing L-zeolite was then rinsed, calcined, and reduced as before. The finished catalyst contained about 0.7 wt.% platinum and had a surface-deposited alkali metal index of about 28. This catalyst, because of the low index value, was not in accordance with the invention. However, this catalyst was tested in Run B as described below in Example V.
EXAMPLE III
A third catalyst was prepared in this example. A potassium form of L-zeolite was subjected to ion exchange with a platinum and KCl-containing ion exchange solution. Before ion exchange, the platinum-containing L-zeolite was subjected to substantial washing in deionized water to assure removal of surface-deposited potassium which might be on the zeolite. The L-zeolite was then calcined and reduced as before. The finished catalyst contained about 1.3 wt.% platinum and had a surface-deposited alkali metal index of about 7. Again, because of the low index value, this catalyst is not of the present invention. This catalyst was also tested in Run C as described in Example V.
EXAMPLE IV
A fourth catalyst was prepared by slurrying 50 grams of potassium form L-zeolite with an aqueous solution of K.sub.2 CO.sub.3. The potassium/zeolite solution was evaporated to dryness and was subjected to calcination as before. Thereafter, the potassium impregnated zeolite was subjected to an ion exchange step for the deposition of platinum. The ion exchange solution comprised a solution of Pt(NH.sub.3).sub.4 Cl.sub.2 /KCl. The resulting composite was thereafter rinsed, calcined and reduced as in the above examples. The resulting catalyst contained about 0.6 wt.% platinum and had a surface-deposited alkali metal index of about 89. This catalyst was made in accordance with the invention and was tested in Run D as described in Example V.
EXAMPLE V
The above four catalysts described in Examples I, II, III, and IV were all subjected to a test to measure their respective performance as dehydrocyclization catalysts. The run numbers for each catalyst are A, B, C, and D, respectively. The results of this test are set forth in the FIGURE. The FIGURE is a plot of catalyst selectivity for the production of aromatics as a function of the surface-deposited alkali metal index.
The charge stock utilized in each run of this example had the following analysis:
______________________________________C.sub.3 /C.sub.4 /C.sub.5 paraffins 0.4 wt. %C.sub.6 paraffins 69.5 wt. %C.sub.6 naphthenes 0.7 wt. %C.sub.7 paraffins 21.4 wt. %C.sub.7 naphthenes 8.0 wt. %Total 100.0 wt. %______________________________________
The tests were run in a pilot plant having a reactor in which the catalyst to be tested was emplaced. The reactor effluent was analyzed by means of an on-line gas chromatograph.
The conditions employed during testing of the catalysts were a reaction zone inlet temperature of 500.degree. C., a 1.0 hr.sup.-1 liquid hourly space velocity, and a reaction zone pressure of 50 psig. Hydrogen was admixed with the charge stock prior to contact with the catalysts. Sufficient hydrogen on a once-through basis was used to provide a 5:1 ratio of moles of hydrogen to moles of hydrocarbon charge stock. The procedure followed in testing was to first contact the catalyst with the charge stock at a reaction zone temperature of 410.degree. C. The 410.degree. C. reaction zone inlet temperature was maintained for a period of 7 hours. Thereafter, the reaction zone inlet temperature was increased to 500.degree. C. over a 3-hour period. The 500.degree. C. temperature was then maintained over a 12-hour test period during which the reaction zone effluent was analyzed by the on-line gas chromatograph each hour.
Results from the test runs are set forth in the FIGURE. For purposes of the FIGURE and the following discussion, selectivity is defined as the grams of aromatics produced per gram of feed converted multiplied by 100. Surprisingly and unexpectedly, it can be seen from the data in the FIGURE that the aromatic selectivity is a strong function of the surface-deposited alkali metal index. Highest aromatic selectivities are obtained for Runs A and D, both employing catalysts made in accordance with the invention.
EXAMPLE VI
Two further catalysts were prepared substantially in accordance with the preparations heretofore set forth. Platinum was deposited by ion exchange on the L-zeolite utilizing a solution of Pt(NH.sub.3).sub.4 Cl.sub.2 ; however, the ion exchange of one of the catalysts was conducted at 25.degree. C. while that of the other catalyst was at 95.degree. C. The platinum contents of the catalysts were 1.38 and 1.55, respectively. The catalysts also contained sufficient surface-deposited potassium to have surface-deposited alkali metal indexes of 129 and 45, respectively.
EXAMPLE VII
In order to determine their selectivities for the production of aromatics in dehydrocyclization, the catalyst from Example VI was tested in Runs E and F using substantially the same test set forth in Example V utilizing the same charge stock. However, in this example, instead of using hydrogen on a once-through basis, the hydrogen admixed with the charge stock was recycle hydrogen recovered from the reaction zone effluent. Additionally, in this test, the reaction zone pressure was 100 psig and not 50 psig as in Example V.
Under the above-described test conditions, both catalysts exhibited high selectivity for the production of aromatics from a highly paraffinic feed. Run E exhibited an aromatic selectivity of 70% and Run F exhibited an aromatic selectivity of 62%. Of special interest is the fact that both catalysts exhibit high selectivities for aromatic production.
EXAMPLE VIII
Two additional catalysts were prepared to evaluate how the L-zeolite is affected when using high pH alkali metal solutions. Both catalysts were prepared in substantially the same manner with the primary difference being the concentration of the alkali metal salt. In the first case, a 50 wt.% KOH solution having a pH of about 15 was used, and for the second catalyst, a 10 wt.% KOH solution having a pH of about 14.2 was used. For each preparation, a quantity of nonacidic L-zeolite was soaked and continuously stirred in the KOH, rinsed with deionized water until the wash water effluent had a pH less than 10.5, dried, and loaded with platinum via the ion exchange procedure as set forth hereinabove. The KOH soak time and temperature was 18 hr/110.degree. C. and 3 days/25.degree. C. for the 50 wt.% KOH and 10 wt.% KOH samples, respectively.
It was found that the two KOH treatments had a surprising and unexpected destructive affect on the L-zeolite. This was evidenced by dissolution of the zeolite such that 77 wt.% of the starting zeolite was lost for the preparation using the 50 wt.% KOH solution and greater than 45 wt.% of the starting zeolite was lost when the 10 wt.% KOH solution was used. Further, it was determined by Si-29 NMR analysis that the 50 wt.% KOH treatment completely destroyed all zeolite crystallinity, converting the remaining solid material to a non-porous silica-alumina, Kaliophilite (KAlSiO.sub.3). X-ray analysis of the catalyst prepared using the 10 wt.% KOH solution showed approximately 2% loss in zeolite crystallinity and a 0.04 expansion in the a.sub.o lattice dimension indicative of silica loss from the zeolite framework. Pilot plant evaluation was not performed on either of these two catalyst preparations because of the destructive affect of the preparation procedure. It is also important to note that neither catalyst is made in accordance with the instant invention.

Catalytic process for the conversion of hydrocarbons

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