Title of Invention	METHOD OF MAKING CATALYST COMPOSITION
Abstract	A method of making a catalyst composition, comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. In an embodiment, the ammonium halide precursor is represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. In an embodiment, the ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where Rf is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each Rf may be the same or different. A process for aromatizing a hydrocarbon using said catalyst composition.

Title of Invention

METHOD OF MAKING CATALYST COMPOSITION

Abstract

A method of making a catalyst composition, comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. In an embodiment, the ammonium halide precursor is represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. In an embodiment, the ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where Rf is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each Rf may be the same or different. A process for aromatizing a hydrocarbon using said catalyst composition.

Full Text	AROMATIZATION CATALYST AND METHODS OF MAKING AND USING SAME FIELD OF THE INVENTION [0001] The present invention relates to an aromatization catalyst and associated methods of making and using same, wherein the catalyst comprises a large pore zeolite support impregnated with a platinum precursor and at least one organic ammonium halide precursor. BACKGROUND [0002] Large pore zeolite catalysts are useful to dehydrocyclize aliphatic hydrocarbons to produce aromatic hydrocarbons. For example, large pore catalysts are useful for reforming petroleum naphtha (e.g., C6-C8) into benzene, toluene, and xylenes. Examples of such aromatization catalysts include large pore zeolite supports impregnated with a mixture of tetraamineplatinum chloride, ammonium chloride (NH4CI) and ammonium fluoride (NH4F). Due to the commercial importance of such catalysts, an ongoing need exists from improved aromatization catalysts and methods of making and using same. SUMMARY OF THE INVENTION [0003] Disclosed herein is a method of making a catalyst composition, comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. In an embodiment, the ammonium halide precursor is represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. In an embodiment, the ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula NfR'^OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. In an embodiment the organic ammonium halide precursor comprises (a) a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and (b) at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where R* is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. [0004] Disclosed herein is a process for aromatizing a hydrocarbon, comprising contacting hydrocarbons with a catalyst under suitable reaction conditions for aromatizing the hydrocarbons, wherein the catalyst is formed by a process comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. [0005] Other aspects and features of the invention will become apparent from review of the detailed description and the claims. DETAILED DESCRIPTION OF THE INVENTION [0006] In an embodiment, the organic ammonium halide precursor comprises one or more compounds represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different. In an embodiment, R is selected from the group consisting of methyl, ethyl, propyl, butyl, and combinations thereof, more specifically methyl. Examples of suitable organic ammonium precursor is represented by the formula N(R)4X include tetraalkylammonium halides such as tetramethylammonium chloride, tetramethylammonium fluoride, tetraethylammonium chloride, tetraethylammonium fluoride, tetrapropylammonium chloride, tetrapropylammonium fluoride, tetrabutylammonium chloride, tetrabutylammonium fluoride, methyltriethylammonium chloride, methyltriethylammonium fluoride, and combinations thereof. [0007] In an embodiment, the organic ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. In an embodiment, R' is selected from the group consisting of methyl, ethyl, propyl, butyl, and combinations thereof, more specifically methyl. Examples of suitable ammonium hydroxide represented by the formula N(R')4OH include ammonium hydroxide, tetraalkylammonium hydroxides such as tetramethylammonium hydroxide, tetraethylammonium hydroxide, tetrapropylammonium hydroxide, tetrabutylammonium hydroxide, and combinations thereof. Examples of suitable acid halides include HCI, HF, HBr, HI, or combinations thereof. [0008] In an embodiment the organic ammonium halide precursor comprises (a) as described previously, a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and (b) as described previously, at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where R' is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R1 may be the same or different. [0009] The halide precursor may further comprise an ammonium halide such as ammonium chloride, ammonium fluoride, or both in various combinations with the organic ammonium halide precursor compounds described previously. More specifically, ammonium chloride, ammonium fluoride, or both may be used with (a) as described previously, a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and/or (b) as described previously, at least one acid halide and at least one organic ammonium hydroxide represented by the formula N(R')4OH, where R' is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. For example, a first fluoride or chloride precursor can be introduced as a tetraalkylammonium halide with a second fluoride or chloride precursor introduced as an ammonium halide. In an embodiment, tetraalkylammonium chloride is used with ammonium fluoride. [0010] Supports for aromatizaton catalysts can generally include any inorganic oxide. These inorganic oxides include bound large pore aluminosilicates (zeolites), amorphous inorganic oxides and mixtures thereof. Large pore aluminosilicates include, but are not limited to, L-zeolite, Y-zeolite, mordenite and the like. Amorphous inorganic oxides include, but are not limited to, aluminum oxide, silicon oxide and titania. Suitable bonding agents for the inorganic oxides include, but are not limited to, silica, alumina, clays, titania and magnesium oxide. #011] Zeolite materials, both natural and synthetic, are known to have catalytic properties for many hydrocarbon processes. Zeolites typically are ordered porous crystalline aluminosilicates having structure with cavities and channels interconnected by channels. The cavities and channels throughout the crystalline material generally can be of a size to allow selective separation of hydrocarbons. [0012] The term "zeolite" generally refers to a particular group of hydrated, crystalline metal aluminosilicates. These zeolites exhibit a network of SiCU and AIO4 tetrahedra in which aluminum and silicon atoms are crosslinked in a three-dimensional framework by sharing oxygen atoms. In the framework, the ratio of oxygen atoms to the total of aluminum and silicon atoms is equal to 2. The framework exhibits a negative electrovalence which typically is balanced by the inclusion of cations within the crystal such as metals, alkali metals, alkaline earth metals or hydrogen. [0013] L-type zeolite catalysts are a sub-group of zeolitic catalysts. Typical L-type zeolites contain mole ratios of oxides in accordance with the following formula: M .2/nO« Al .2O3«xSiO2«yH .2O wherein "M" designates at least one exchangeable cation such as barium, calcium, cerium, lithium, magnesium, potassium, sodium, strontium, and zinc as well as non-metallic cations like hydronium and ammonium ions which may be replaced by other exchangeable cations without causing a substantial alteration of the basic crystal structure of the L-type zeolite. The "n" in the formula represents the valence of "M", "x" is 2 or greater; and "y" is the number of water molecules contained in the channels or interconnected voids with the zeolite. [0014] Bound potassium L-type zeolites, or KL zeolites, have been found to be particularly desirable. The term KL zeolite as used herein refers to L-type zeolites in which the principal cation M incorporated in the zeolite is potassium. As used in this application, a KL zeolite is one that has not been significantly cation-exchanged or impregnated with another metal unless the term KL zeolite is preceded by a modifier such as "platinum-impregnated" or the zeolite explicitly is referred to as a "KL supported Pt zeolite catalyst." [0015] The platinum precursor can be any decomposable platinum compound. Examples of such compounds include, but are not limited to, ammonium tetrachloroplatinate, chloroplatinic acid, diammineplatinum (II) nitrite, bis- t (ethylenediamine)platinum (II) chloride, platinum (II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride, tetraammineplatinum (II) hydroxide, tetraammineplatinum chloride, and tetraammineplatinum (II) nitrate. [0016] In an embodiment, a method for making an aromatization catalyst composition comprises the following steps: (1) predrying large pore zeolite support; (2) treating the zeolite support by impregnating the support with platinum and halide precursors; (3) optionally aging the impregnated support; (4) optionally drying the support; and (5) calcining the support. [0017] Prior to impregnation, the zeolite support typically is dried under flowing or stationary gas selected from the group consisting of hydrogen, oxygen, air, helium, nitrogen, argon, and mixtures thereof. As an example, in some cases the gas can be air, and the drying can be performed from about 1 minute to about 20 hours and at a temperature from about 100° to about 600° C. Impregnation of the halide and platinum precursors into the zeolite support may be performed by any suitable method as known to those skilled in the art, such as insipient wetness. [0018] In some embodiments, it may be desirable to age the impregnated catalyst support. This aging can be performed at temperatures from about subambient to about 200°C, at pressures from about ambient to about 500 psig for periods of time from about 1 minute to about 10 days and under conditions where the impregnated solid is stationary or moving. Ambient conditions are defined as environmental temperature at atmospheric pressure. [0019] In some embodiments, it may be desirable to dry the impregnated catalyst support. The drying generally occurs in the presence of a gas, which can be air, oxygen, nitrogen, hydrogen, or any inert gas, or mixtures thereof. As an example, it may be desirable to dry the impregnated catalyst in the presence of a gas comprising nitrogen and/or oxygen, for example enriched air or diluted air, such that it contains from about 0.1 vol % to about 100 vol % nitrogen, alternatively from about 0.1 vol % to about 60 vol % nitrogen, alternatively from about 0.1 vol % to about 30 vol % nitrogen. In an embodiment, the gas is a mixture of air and nitrogen. This drying can be performed at temperatures from about 0° to about 300°C, alternatively from about 25° to about 250°C, alternatively from about 50° to about 200°C, and at pressures from about 0.01 mmHg to about 500 psig, alternatively from about 0.01 mmHg to about 50 psig, alternatively from about 0.01 mmHg to about 5 psig, alternatively at subambient pressure, also referred to as vacuum drying; for periods of time from about 1 minute to about 20 hours; under conditions where the gas is stationary or moving; and under conditions where the impregnated solid is either stationary or moving. During the drying step, the temperature can be optionally increased from ambient temperature to the desired drying temperature in a controlled manner, preferably through a series of temperature increases followed by temperature hold periods. The drying step may be carried out in any suitable drying equipment, for example a rotary drier. [0020] In some embodiments, it may be desirable to calcine the impregnated catalyst support. The calcination generally occurs in the presence of a gas, which can be air, oxygen, nitrogen, hydrogen, or any inert gas, or mixtures thereof. As an example, it may be desirable to calcine in the presence of a gas comprising nitrogen and/or oxygen, for example enriched air or diluted air, such that it contains from about 0.1 vol % to about 100 vol % oxygen, alternatively from about 1 vol % to about 80 vol % oxygen, alternatively from about 5 vol % to about 60 vol % oxygen. In an embodiment, the gas is a mixture of air and nitrogen, for example having a volume ratio air to nitrogen of from about 1:1 to about 1:3. The calcination step can be performed at temperatures from about 50° to about 600°C, alternatively from about 160° to about 550°C, alternatively from about 275° to about 500°C; under pressures from ambient to 500 psig; for periods of time from about 1 minute to about 100 hours; under conditions where the gas is stationary or moving; and under conditions were the impregnated catalyst support is stationary or moving. During the calcination step, the temperature is increased from ambient temperature in a controlled manner, preferably through a series of temperature increases followed by temperature hold periods. The calcining step may be carried out in any suitable calcining equipment, for example a rotary calciner or a belt conveyed calciner. [0021] In an embodiment, a KL-zeolite supported platinum aromatization catalyst is prepared by impregnating a KL-zeolite-support with tetramethylammonium chloride (TMAC), and/or tetramethylammonium fluoride (TMAF), and tetraamineplatinum chloride (TAPC); and calcinating the impregnated zeolite. In an embodiment, a KL-zeolite supported platinum aromatization catalyst is prepared by impregnating a KL-zeolite-support with ammonium fluoride, tetramethylammonium chloride (TMAC), and tetraamineplatinum chloride (TAPC); and calcinating the impregnated zeolite. [0022] In another aspect, the invention provides a process for reforming a hydrocarbon, for example aromatization, isomerization, dehydrogenation, and combinations thereof. For example, such a process could include contacting a hydrocarbon stream with a catalyst as described herein under suitable reaction conditions for aromatization of hydrocarbons, for example a temperature in the range of about 800° F to about 1050° F. In an embodiment, hydrogen is recovered as a product from the reforming process. In an embodiment, the catalyst comprises a composition made according to one of the methods described herein. [0023] In some embodiments, it may be desirable to provide a catalyst having less than about 1.3 wt% chlorine, alternatively less thpn about 1.0 wt% chlorine, alternatively less than about 0.5 wt% chlorine. In other embodiments, it may be desirable to provide a catalyst having less than about 1.3 wt% fluorine, alternatively less than about 1.0 wt% fluorine, alternatively less than about 0.5 wt% fluorine. Similarly, in other embodiments, it may be desirable to provide a catalyst having less than about 1.0 wt% platinum, alternatively less than about 0.6 wt% platinum, alternatively from about 0.2 to about 0.7 wt% platinum. In various embodiments, the atomic ratio of Pt : F : Cl in the catalyst is from about 1-0.5 : 3.3-1.7 : 10-5, respectively. As an example, the amount of fluorine, chlorine, and/or platinum in the catalyst can be controlled by controlling the amount of the respective precursors in the impregnation treatment. [0024] In various embodiments, the catalyst composition comprises less than or equal to about 1 wt% platinum and has a Teo temperature of less than about 960°F and/or a deactivation rate of less than about 2.4 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.5 °F/day. [0025] In various embodiments, the catalyst composition comprises less than or equal to about 0.5 wt% platinum and has a T6o temperature of less than about 1010°F and/or a deactivation rate of less than about 36 °F/day, alternatively a T60 temperature of less than about 965°F and/or a deactivation rate of less than about 3.5 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.2 °F/day. 1 I [0026] In various embodiments, the catalyst composition comprises less than or equal to about 0.3 wt% platinum and has a T6o temperature of less than about 972°F and/or a deactivation rate of less than about 11.4 °F/day, alternatively a T6o temperature of less than about 950°F and/or a deactivation rate of less than about 1.5 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.2 °F/day. The T60 temperature is defined as the temperature for a given feedstock at which the sum of the benzene wt% and toluene wt% in the reactor effluent is 60 wt%. Once this conversion rate is achieved at T6o, the deactivation rate is defined as a degree increase in temperature per day to maintain this conversion rate. EXAMPLES [0027] In each of the following examples, the prepared catalysts were ground, sieved to 20-40 mesh, and placed in a reactor comprising a metal reactor vessel in a temperature controlled furnace. After reducing the catalyst under flowing hydrogen, a feed stream of aliphatic hydrocarbon and hydrogen was introduced to the reactor vessel at a feed rate of 22mL/min and a pressure of 50 psig to obtain performance data. The reactor effluent composition was analyzed by gas chromatography to indicate the amount of benzene and toluene. [0028] The catalysts prepared in accordance with Examples 1-11 below illustrate effects of varying the amount of platinum impregnated into the KL-zeolite catalyst when compared to Aromax® II catalyst. Under the present invention, significantly lower T6o values and deactivation rates can be obtained by preparing KL supported Pt zeolite catalysts using TMAF in place of NH4F and using a tetraalkylammonium chloride in place of NH4CI. The results are summarized in Table 1. Example 1 [0029] A platinum-impregnated KL-zeolite catalyst containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.45g TMAF, 0.1 Og TMAC and 2.50g water is formed and added to a container containing 5.0g of a silica bound KL-zeolite extrudates that has been calcined for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp rate is 0.25°C/min). The resultant catalyst contains 1.07 wt% Pt, 1.02 wt% Cl and 1.0 wt% F. Example 2 (comparison) [0030] A platinum-impregnated KL-zeolite catalyst containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.1 Og NH4F, and 0.05g NH4CI is formed and added to a container containing 5.0g of a silica bound KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp rate is 0.25°C/min). The resulting catalyst contains 0.55 wt% Pt, 0.5 wt% Cl and 1.0 wt% F. Example 3 [0031] A platinum-impregnated KL-zeolite catalyst containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.1 Og TMAC and 2.50g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp rate is 0.25°C/min). The resulting catalyst contains 0.54 wt% Pt, 0.83 wt% Cl and 1.0 wt% F. Example 4 (comparison) [0032] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.40g NH4F, and 0.8g NH4CI (0.8% aqueous solution) is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours ambient temperature. The impregnated KL-zeolite is dried in a vacuum for four hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.34 wt% Cl and 1.1 wt% F. Example 5 [0033] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.40g NH4F, and 0.14g TMAC is formed and added to a container containing 18.23g of a I t KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours ambient temperature. The impregnated KL-zeolite is dried in a vacuum for four hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cland1.12wt%F. Example 6 [0034] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.78g TMAF, 0.1 Og TMAC and 6.90g water is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.30 wt% Cl and 1.12 wt% F. Example 7 [0035] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.84g TMAF, and 7g NH4CI is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.31 wt% Cl and 1.15 wt% F. Example 8 [0036] A platinum-impregnated KL-zeolite catalyst containing 0.29 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1g TAPC, 1.60g TMAF and 0.11g TMAC is formed and added to a container containing 18.22g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.29 wt% Pt, 0.30 wt% Cl and 1.00 wt% F. [0037] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 2.05g TMAF and 0.1 Og TMAC is formed and added to a container containing 18.25g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30,wt% Pt, 0.30 wt% Cl and 1.28 wt% F. Example 10 [0038] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.75g TMAF, 0.18g tetraethylammonium chloride (TEAC) and 6.50g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cl and 1.09 wt% F. Example 11 [0039] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.75g TMAF, 0.30g tetrabutylammonium chloride (TBAC) and 6.50g water is formed and added to a container containing 18.29g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cl and 1.09 wt% F. * Temperature (°F) at which the sum of the benzene wt% and toluene wt% in the reactor effluent is 60 wt%. [0040] The results in Table 1 demonstrate that the substitution of TMAF and TMAC for NH4F and NH4CI, respectively, significantly decreases the deactivation rate and/or the T6o value. Example 1 used an impregnation comprising TAPC, TMAC and TMAF and produced a 1.0 wt% Pt. When compared to the Aromax® II catalyst, there was a 24° F reduction in the T6o value. By reducing the amount of platinum from 1.0 wt% to 0.5 wt%, as shown in the comparison of Examples 2 and 3, the catalyst made using TAPC, NH4F and NH4CI (Example 2) had a 75° F increase in the T6o value and a significant increase in the deactivation rate when compared to the Aromax® II catalyst which contained 1 wt% platinum. [0041] While the catalyst containing 0.5 wt% platinum made by using TAPC, TMAF and TMAC (Example 3) did not show improvement over the Aromax® II catalyst with respect to the T6o value or the deactivation rate, the catalyst was a significant improvement over Example 2 which is an Aromax® II type catalyst, but containing 0.5 wt% platinum. [0042] Examples 4 and 6 show the differences between Aromax® II catalyst and an Aromax® II type catalyst containing 0.3 wt% platinum and a catalyst prepared using TAPC, TMAF and TMAC containing 0.3 wt% platinum. The Aromax® II type catalyst (Example 4) showed a significant increase in the T6o value and in the deactivation rate when compared to the Aromax® II catalyst (comparison) and a platinum-impregnated KL-zeolite catalyst of the invention made in accordance with Example 6. [0043] Example 4 and 5 show the differences between an Aromax® II type catalyst containing 0.3 wt% platinum and a catalyst prepared using TAPC, NH4F, and TMAC containing 0.3 wt% platinum. The Aromax® II type catalyst (Example 4) showed a significant increase in the deactivation rate when compared to the platinum-impregnated KL-zeolite catalyst of the invention made in accordance with Example 5. [0044] Examples 7-11 show improved T6o values and lower deactivation rates than comparative Example 4 when TMAF was substituted for NH4F. Examples 8 and 9 show the effects of fluorine and chlorine loading, as shown in more detail below. 10045] Examples 3, 12, 13, and 14 in Table 2 illustrate effects on T6o value and the deactivation rate when the amount of chlorine in the catalyst is varied. Examples 12,13, and 14 were prepared as follows: Example 12 [0046] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.02g TMAC and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. Example 13 [0047] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.05g TMAC and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. Example 14 [0048] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. [0049] Table 2 is a comparison of changes in the chlorine content of catalyst prepared using TAPC, TMAF and TMAC. The results demonstrate a progressively lower deactivation rate and T6o value as chlorine levels are reduced. Example 2 demonstrates that a poor T6o value and deactivation rate are obtained when the impregnate comprises NH4F and NH4CI instead of TMAF and TMAC. [0050] Examples 15-23 (in addition to Examples 6-11) set forth procedures for preparing KL supported Pt zeolite aromatization catalysts containing about 0.3 wt% platinum. The catalysts produced have varying amounts of fluorine and chlorine. Example 15 [0051] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.08g TMAF and 4.5g water is formed and added to a container containing 9.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 16 [0052] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.16g TAPC, 2.55g TMAF, 8.0g TMAC and 7.0g water is formed and added to a container containing 29.50g of a KL- zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 17 [0053] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.28g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 18 [0054] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.60g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 68 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 19 [0055] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.80g TMAF, 0.049g TMAC and 4.5g water is formed and added to a container containing 9.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 20 [0056] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.78g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 21 [0057] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.92g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 22 [0058] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.50g TAPC, 0.82g TMAF, 0.06g TMAC and 4.0g water is formed and added to a container containing 9.11g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 23 [0059] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.82g TMAF, 0.1 Og TMAC and 4.0g water is formed and added to a container containing 9.11g of a KL-zeolite that has been baked for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. [0060] The Tw and deactivation rate data for the catalysts prepared in accordance with Examples 15 - 23 as well as Examples 6-11 are summarized in Table 3. 1 [0061] The results of Table 3 show that satisfactory T6o values and low deactivation rates can be obtained from a low-platinum load catalyst formed by using the TAPC, TMAF and TMAC impregnate (Examples 16-23) to prepare the catalyst on a KL-zeolite support. The results show further that when TMAF is used in place of NH4F, the catalyst has lower T^ values and lower deactivation rates than catalysts containing 0.3 wt.% and 0.5 wt.% platinum prepared using an impregnate containing TAPC, NH4F and NH4CI. See comparative Examples 2 and 4 in Table 1. [0062] Table 4 is a comparison of changes in the fluorine impregnating agent used to prepare the catalyst. Example 24 [0063] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC and 4.5g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 75°C and then 2 hours at 170°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. Example 25 [0064] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.1 Og ammonium chloride and 4.8g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 10 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 160°C and then calcined at 300°C for another 2 hours. Example 26 [0065] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.20g TMAC and 4.8g water is formed and added to a container containing 10.Og of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 95°C, and then 2 hours at 160°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. Example 27 [0066] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.15g ammonium chloride, 0.2g ammonium fluoride and 4.5g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 70°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours. Example 28 [0067] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 0.1g ammonium fluoride, 0.1 Og TMAC and 2.4g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. [0068] The T6o and deactivation rate data for the catalysts prepared in accordance with Examples 24 - 28 is summarized in Table 4. [0069] The results of Table 4 show that satisfactory T6o values and low deactivation rates can be obtained by using a TAPC, TMAC and ammonium fluoride impregnate to prepare the catalyst on a KL-zeolite support (Example 28). Conversely, where no fluorine impregnate was used (Examples 24-26), or where ammonium fluoride was used in conjunction with ammonium chloride (Example 27), the resulting T6oand deactivation rates were undesirably higher. [0070] In addition to the methods described in the Examples above, the catalysts of the present invention can be prepared by impregnating a suitable catalytic substrate with TAPC with hydrogen fluoride (HF), hydrogen chloride (HCI) and an organic or inorganic hydroxide represented by the formula N(R)4OH, where R represents hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms. Example 29 [0071] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI, 0.83g ammonium hydroxide and 2.0g water is formed and added to a container containing 10.97g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 30 [0072] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI, 2.45g tetramethylammonium hydroxide and 0.50g water is formed and added to a container containing 10.96g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 31 [0073] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI and 2.8g tetraethylammonium hydroxide is formed and added to a container containing 10.96g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. Example 32 [0074] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI and 6.8g tetrapropylammonium hydroxide is formed and added to a container containing 10.93g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours. [0075] The results of Examples 29-32 are summarized in Table 5. This table shows that low loading catalysts containing 0.5 wt% platinum, 1.03 wt% fluorine and 0.39 wt% chlorine prepared using TAPC, HF, HCI and ammonium hydroxide or a tetraalkylammonium hydroxide result in low fouling rates. reactor effluent is 60 wt%. [0076] While the foregoing discussion is intended to provide a detailed illustration of certain embodiments of the invention, it will be appreciated that additional embodiments are also possible under the claims provided herein. It will also be appreciated that numerical values and ranges are presented in approximate form such that small or inconsequential deviations from such values are intended to be within the scope of the values and ranges presented. CLAIMS The following is claimed: 1. A method of making a catalyst composition, comprising: impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. 2. The method of claim 1 wherein the ammonium halide precursor is represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. 3. The method of claim 2 wherein the large pore zeolite is an L-type zeolite. 4. The method of claim 2 wherein the large pore zeolite is a potassium L-type zeolite. 5. The method of claim 2 wherein R is an alkyl. 6. The method of claim 2 wherein R is selected from the group consisting of methyl, ethyl, propyl, butyl, and combinations thereof. 7. The method of claim 2 wherein R is methyl. 8. The method of claim 2 wherein X is selected from the group consisting of F, Cl, Br, I, and combinations thereof. 9. The method of claim 6 wherein X is selected from the group consisting of F, Cl, Br, I, and combinations thereof. 10. The method of claim 2 wherein X is F. 11. The method of claim 2 wherein X is Cl. 12. The method of claim 2 wherein the halide precursor is tetramethylammonium chloride. 13. The method of claim 2 wherein the halide precursor is tetramethylammonium fluoride. 14. The method of claim 12 wherein the halide precursor further comprises tetramethylammonium fluoride. 15. The method of claim 2 wherein the halide precursor further comprises ammonium chloride. 16. The method of claim 12 wherein the halide precursor further comprises ammonium chloride. 17. The method of claim 13 wherein the halide precursor further comprises ammonium chloride. 18. The method of claim 14 wherein the halide precursor further comprises ammonium chloride. 19. The method of claim 2 wherein the halide precursor further comprises ammonium fluoride. 20. The method of claim 12 wherein the halide precursor further comprises ammonium fluoride. 21. The method of claim 13 wherein the halide precursor further comprises ammonium fluoride. 22. The method of claim 14 wherein the halide precursor further comprises ammonium fluoride. 23. The method of claim 15 wherein the halide precursor further comprises ammonium fluoride. 24. The method of claim 16 wherein the halide precursor further comprises ammonium fluoride. 25. The method of claim 17 wherein the halide precursor further comprises ammonium fluoride. 26. The method of claim 18 wherein the halide precursor further comprises ammonium fluoride. 27. The method of claim 2, wherein the platinum precursor is selected from the group consisting of ammonium tetrachloroplatinate, chloroplatinic acid, diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum (II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride, tetraammineplatinum (II) hydroxide, tetraammineplatinum (II) nitrate, and combinations thereof. 28. The method of claim 2 wherein the platinum precursor is tetraamineplatinum chloride. 29. The method of claim 12 wherein the platinum precursor is tetraamineplatinum chloride. 30. The method of claim 13 wherein the platinum precursor is tetraamineplatinum chloride. 31. The method of claim 14 wherein the platinum precursor is tetraamineplatinum chloride. 32. The method of claim 16 wherein the platinum precursor is tetraamineplatinum chloride. 33. The method of claim 17 wherein the platinum precursor is tetraamineplatinum chloride. 34. The method of claim 18 wherein the platinum precursor is tetraamineplatinum chloride. 35. The method of claim 20 wherein the platinum precursor is tetraamineplatinum chloride. 36. The method of claim 21 wherein the platinum precursor is tetraamineplatinum chloride. 37. The method of claim 22 wherein the platinum precursor is tetraamineplatinum chloride. 38. The method of claim 23 wherein the platinum precursor is tetraamineplatinum chloride. 39. The method of claim 24 wherein the platinum precursor is tetraamineplatinum chloride. 40. The method of claim 25 wherein the platinum precursor is tetraamineplatinum chloride. 41. The method of claim 26 wherein the platinum precursor is tetraamineplatinum chloride. 42. The method of claim 1 wherein the ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. 43. The method of claim 42 wherein the large pore zeolite is an L-type zeolite. 44. The method of claim 42 wherein the large pore zeolite is a potassium L-type zeolite. 45. The method of claim 42 wherein R* is an alkyl. 46. The method of claim 42 wherein R' is selected from the group consisting of methyl, ethyl, propyl, butyl, and combinations thereof, 47. The method of claim 42 wherein R1 is methyl. 48. The method of claim 42 wherein the acid halide is HCI, HF, HBr, HI, or combinations thereof. 49. The method of claim 46 wherein the acid halide is HCI, HF, or both. 50. The method of claim 47 wherein the acid halide is HCI. 51. The method of claim 47 wherein the acid halide is HF. 52. The method of claim 42 wherein the halide precursor further comprises ammonium chloride, ammonium fluoride, or both. 53. The method of claim 49 wherein the halide precursor further comprises ammonium chloride, ammonium fluoride, or both. 54. The method of claim 43 wherein the platinum precursor is selected from the group consisting of ammonium tetrachloroplatinate, chloroplatinic acid, diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum (II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride, tetraammineplatinum (II) hydroxide, tetraammineplatinum (II) nitrate, and combinations thereof. 55. The method of claim 42 wherein the platinum precursor is tetraamineplatinum chloride. 56. The method of claim 48 wherein the platinum precursor Is tetraamineplatinum chloride. 57. The method of claim 49 wherein the platinum precursor is tetraamineplatinum chloride. 58. The method of claim 50 wherein the platinum precursor is tetraamineplatinum chloride. 59. The method of claim 51 wherein the platinum precursor is tetraamineplatinum chloride. 60. The method of claim 53 wherein the platinum precursor is tetraamineplatinum chloride. 61. The method of claim 2 wherein the ammonium halide precursor further comprises at least one acid halide and at least one ammonium hydroxide represented by the formula N(RI)4OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R1 may be the same or different. 62. The method of claim 61 wherein the large pore zeolite is a potassium L-type zeolite. 63. The method of claim 61 wherein each R and R1 are selected from the group consisting of methyl, ethyl, propyl, butyl, and combinations thereof. 64. The method of claim 61 wherein X is selected from the group consisting of F, Cl, Br, I, and combinations thereof. 65. The method of claim 61 wherein the acid halide is HCI, HF, or both. 66. The method of claim 61 wherein the halide precursor further comprises ammonium chloride, ammonium fluoride, or both. 67. The method of claim 61 wherein the platinum precursor is selected from the group consisting of ammonium tetrachlorop latin ate, chloroplatinic acid, diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum (II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride, tetraammineplatinum (II) hydroxide, tetraammineplatinum chloride, tetraammineplatinum (II) nitrate, and combinations thereof. 68. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt% chlorine. 69. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt% chlorine. 70. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt% fluorine. 71. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt% fluorine. 72. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt% chlorine and less than about 1.3 wt% fluorine. 73. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt% chlorine and less than about 1.3 wt% fluorine. 74. The method of claim 2, wherein the catalyst comprises platinum in the range of about 0.2 wt% to about 0.7 wt%. 75. The method of claim 42, wherein the catalyst comprises platinum in the range of about 0.2 wt% to about 0.7 wt%. 76. The method of claim 2, wherein the catalyst comprises less than about 0.6 wt% platinum, less than about 1.3 wt% chlorine, and less than about 1.3 wt% fluorine. 77. The method of claim 42, wherein the catalyst comprises less than about 0.6 wt% platinum, less than about 1.3 wt% chlorine, and less than about 1.3 wt% fluorine. 78. The process of claim 1 wherein the catalyst has a deactivation rate of less than about 2.4 °F/day and a T6o of about 875 to about 975 °F. 79. The process of claim 2 wherein the catalyst has a deactivation rate of less than about 2.4 °F/day and a T6o of about 875 to about 975 °F. 80. The process of claim 42 wherein the catalyst has a deactivation rate of less than about 2.4 °F/day and a T6o of about 875 to about 975 °F. 81. The process of claim 61 wherein the catalyst has a deactivation rate of less than about 2.4 °F/day and a T6o of about 875 to about 975 °F. 82. A method of making a catalyst composition, comprising: impregnating a large pore zeolite support with a platinum precursor; at least one acid halide; and at least one organic ammonium hydroxide represented by the formula NfR'^OH, where R' is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. 83. A method of making a catalyst composition, comprising: impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. 84. A composition made according to the method of claim 1. 85. A process for reforming a hydrocarbon, comprising: contacting hydrocarbons with a catalyst under suitable reaction conditions for aromatizing the hydrocarbons, wherein the catalyst is formed by a process comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. 86. The process of claim 85 wherein the catalyst has a deactivation rate of less than about 2.4 °F/day and a T6o of about 875 to about 975 °F. 87. The process of claim 85 further comprising recovering hydrogen. 88. The process of claim 82 further comprising vacuum drying the impregnated catalyst support. 89. The process of claim 83 further comprising vacuum drying the impregnated catalyst support. 90. The process of claim 82 further comprising calcining the impregnated catalyst support in air having a diluted oxygen content. 91. The process of claim 83 further comprising calcining the impregnated catalyst support in air having a diluted oxygen content. 92. The process of claim 88 further comprising calcining the impregnated catalyst support in air having a diluted oxygen content. 93. The process of claim 89 further comprising calcining the impregnated catalyst support in air having a diluted oxygen content.

Full Text

AROMATIZATION CATALYST AND METHODS OF MAKING AND USING SAME
FIELD OF THE INVENTION
[0001] The present invention relates to an aromatization catalyst and associated methods of making and using same, wherein the catalyst comprises a large pore zeolite support impregnated with a platinum precursor and at least one organic ammonium halide precursor.
BACKGROUND
[0002] Large pore zeolite catalysts are useful to dehydrocyclize aliphatic hydrocarbons to produce aromatic hydrocarbons. For example, large pore catalysts are useful for reforming petroleum naphtha (e.g., C6-C8) into benzene, toluene, and xylenes. Examples of such aromatization catalysts include large pore zeolite supports impregnated with a mixture of tetraamineplatinum chloride, ammonium chloride (NH4CI) and ammonium fluoride (NH4F). Due to the commercial importance of such catalysts, an ongoing need exists from improved aromatization catalysts and methods of making and using same.
SUMMARY OF THE INVENTION
[0003] Disclosed herein is a method of making a catalyst composition, comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor. In an embodiment, the ammonium halide precursor is represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different. In an embodiment, the ammonium halide precursor comprises at least one acid halide and at least one ammonium hydroxide represented by the formula NfR'^OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. In an embodiment the organic ammonium halide precursor comprises (a) a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and (b) at least one acid halide and at least one ammonium

hydroxide represented by the formula N(R')4OH, where R* is hydrogen or a
substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms
wherein each R' may be the same or different.
[0004] Disclosed herein is a process for aromatizing a hydrocarbon, comprising
contacting hydrocarbons with a catalyst under suitable reaction conditions for
aromatizing the hydrocarbons, wherein the catalyst is formed by a process
comprising impregnating a large pore zeolite support with a platinum precursor and
at least one organic ammonium halide precursor.
[0005] Other aspects and features of the invention will become apparent from
review of the detailed description and the claims.
DETAILED DESCRIPTION OF THE INVENTION
[0006] In an embodiment, the organic ammonium halide precursor comprises one
or more compounds represented by the formula N(R)4X, where X is a halide and
where R represents a hydrogen or a substituted or unsubstituted carbon chain
molecule having 1-20 carbons wherein each R may be the same or different. In an
embodiment, R is selected from the group consisting of methyl, ethyl, propyl, butyl,
and combinations thereof, more specifically methyl. Examples of suitable organic
ammonium precursor is represented by the formula N(R)4X include
tetraalkylammonium halides such as tetramethylammonium chloride,
tetramethylammonium fluoride, tetraethylammonium chloride, tetraethylammonium
fluoride, tetrapropylammonium chloride, tetrapropylammonium fluoride,
tetrabutylammonium chloride, tetrabutylammonium fluoride,
methyltriethylammonium chloride, methyltriethylammonium fluoride, and combinations thereof.
[0007] In an embodiment, the organic ammonium halide precursor comprises at
least one acid halide and at least one ammonium hydroxide represented by the
formula N(R')4OH, where R1 is hydrogen or a substituted or unsubstituted carbon
chain molecule having 1-20 carbon atoms wherein each R' may be the same or
different. In an embodiment, R' is selected from the group consisting of methyl, ethyl,
propyl, butyl, and combinations thereof, more specifically methyl. Examples of
suitable ammonium hydroxide represented by the formula N(R')4OH include
ammonium hydroxide, tetraalkylammonium hydroxides such as
tetramethylammonium hydroxide, tetraethylammonium hydroxide,

tetrapropylammonium hydroxide, tetrabutylammonium hydroxide, and combinations thereof. Examples of suitable acid halides include HCI, HF, HBr, HI, or combinations thereof.
[0008] In an embodiment the organic ammonium halide precursor comprises (a) as described previously, a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and (b) as described previously, at least one acid halide and at least one ammonium hydroxide represented by the formula N(R')4OH, where R' is hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R1 may be the same or different.
[0009] The halide precursor may further comprise an ammonium halide such as ammonium chloride, ammonium fluoride, or both in various combinations with the organic ammonium halide precursor compounds described previously. More specifically, ammonium chloride, ammonium fluoride, or both may be used with (a) as described previously, a compound represented by the formula N(R)4X, where X is a halide and where R represents a hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbons wherein each R may be the same or different and/or (b) as described previously, at least one acid halide and at least one organic ammonium hydroxide represented by the formula N(R')4OH, where R' is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different. For example, a first fluoride or chloride precursor can be introduced as a tetraalkylammonium halide with a second fluoride or chloride precursor introduced as an ammonium halide. In an embodiment, tetraalkylammonium chloride is used with ammonium fluoride. [0010] Supports for aromatizaton catalysts can generally include any inorganic oxide. These inorganic oxides include bound large pore aluminosilicates (zeolites), amorphous inorganic oxides and mixtures thereof. Large pore aluminosilicates include, but are not limited to, L-zeolite, Y-zeolite, mordenite and the like. Amorphous inorganic oxides include, but are not limited to, aluminum oxide, silicon oxide and titania. Suitable bonding agents for the inorganic oxides include, but are not limited to, silica, alumina, clays, titania and magnesium oxide.

#011] Zeolite materials, both natural and synthetic, are known to have catalytic properties for many hydrocarbon processes. Zeolites typically are ordered porous crystalline aluminosilicates having structure with cavities and channels interconnected by channels. The cavities and channels throughout the crystalline material generally can be of a size to allow selective separation of hydrocarbons. [0012] The term "zeolite" generally refers to a particular group of hydrated, crystalline metal aluminosilicates. These zeolites exhibit a network of SiCU and AIO4 tetrahedra in which aluminum and silicon atoms are crosslinked in a three-dimensional framework by sharing oxygen atoms. In the framework, the ratio of oxygen atoms to the total of aluminum and silicon atoms is equal to 2. The framework exhibits a negative electrovalence which typically is balanced by the inclusion of cations within the crystal such as metals, alkali metals, alkaline earth metals or hydrogen.
[0013] L-type zeolite catalysts are a sub-group of zeolitic catalysts. Typical L-type zeolites contain mole ratios of oxides in accordance with the following formula:
M .2/nO« Al .2O3«xSiO2«yH .2O
wherein "M" designates at least one exchangeable cation such as barium, calcium, cerium, lithium, magnesium, potassium, sodium, strontium, and zinc as well as non-metallic cations like hydronium and ammonium ions which may be replaced by other exchangeable cations without causing a substantial alteration of the basic crystal structure of the L-type zeolite. The "n" in the formula represents the valence of "M", "x" is 2 or greater; and "y" is the number of water molecules contained in the channels or interconnected voids with the zeolite.
[0014] Bound potassium L-type zeolites, or KL zeolites, have been found to be particularly desirable. The term KL zeolite as used herein refers to L-type zeolites in which the principal cation M incorporated in the zeolite is potassium. As used in this application, a KL zeolite is one that has not been significantly cation-exchanged or impregnated with another metal unless the term KL zeolite is preceded by a modifier such as "platinum-impregnated" or the zeolite explicitly is referred to as a "KL supported Pt zeolite catalyst."
[0015] The platinum precursor can be any decomposable platinum compound. Examples of such compounds include, but are not limited to, ammonium tetrachloroplatinate, chloroplatinic acid, diammineplatinum (II) nitrite, bis-

t
(ethylenediamine)platinum (II) chloride, platinum (II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride, tetraammineplatinum (II) hydroxide, tetraammineplatinum chloride, and tetraammineplatinum (II) nitrate. [0016] In an embodiment, a method for making an aromatization catalyst composition comprises the following steps: (1) predrying large pore zeolite support; (2) treating the zeolite support by impregnating the support with platinum and halide precursors; (3) optionally aging the impregnated support; (4) optionally drying the support; and (5) calcining the support.
[0017] Prior to impregnation, the zeolite support typically is dried under flowing or stationary gas selected from the group consisting of hydrogen, oxygen, air, helium, nitrogen, argon, and mixtures thereof. As an example, in some cases the gas can be air, and the drying can be performed from about 1 minute to about 20 hours and at a temperature from about 100° to about 600° C. Impregnation of the halide and platinum precursors into the zeolite support may be performed by any suitable method as known to those skilled in the art, such as insipient wetness. [0018] In some embodiments, it may be desirable to age the impregnated catalyst support. This aging can be performed at temperatures from about subambient to about 200°C, at pressures from about ambient to about 500 psig for periods of time from about 1 minute to about 10 days and under conditions where the impregnated solid is stationary or moving. Ambient conditions are defined as environmental temperature at atmospheric pressure.
[0019] In some embodiments, it may be desirable to dry the impregnated catalyst support. The drying generally occurs in the presence of a gas, which can be air, oxygen, nitrogen, hydrogen, or any inert gas, or mixtures thereof. As an example, it may be desirable to dry the impregnated catalyst in the presence of a gas comprising nitrogen and/or oxygen, for example enriched air or diluted air, such that it contains from about 0.1 vol % to about 100 vol % nitrogen, alternatively from about 0.1 vol % to about 60 vol % nitrogen, alternatively from about 0.1 vol % to about 30 vol % nitrogen. In an embodiment, the gas is a mixture of air and nitrogen. This drying can be performed at temperatures from about 0° to about 300°C, alternatively from about 25° to about 250°C, alternatively from about 50° to about 200°C, and at pressures from about 0.01 mmHg to about 500 psig, alternatively from about 0.01 mmHg to about 50 psig, alternatively from about 0.01 mmHg to about 5 psig,

alternatively at subambient pressure, also referred to as vacuum drying; for periods of time from about 1 minute to about 20 hours; under conditions where the gas is stationary or moving; and under conditions where the impregnated solid is either stationary or moving. During the drying step, the temperature can be optionally increased from ambient temperature to the desired drying temperature in a controlled manner, preferably through a series of temperature increases followed by temperature hold periods. The drying step may be carried out in any suitable drying equipment, for example a rotary drier.
[0020] In some embodiments, it may be desirable to calcine the impregnated catalyst support. The calcination generally occurs in the presence of a gas, which can be air, oxygen, nitrogen, hydrogen, or any inert gas, or mixtures thereof. As an example, it may be desirable to calcine in the presence of a gas comprising nitrogen and/or oxygen, for example enriched air or diluted air, such that it contains from about 0.1 vol % to about 100 vol % oxygen, alternatively from about 1 vol % to about 80 vol % oxygen, alternatively from about 5 vol % to about 60 vol % oxygen. In an embodiment, the gas is a mixture of air and nitrogen, for example having a volume ratio air to nitrogen of from about 1:1 to about 1:3. The calcination step can be performed at temperatures from about 50° to about 600°C, alternatively from about 160° to about 550°C, alternatively from about 275° to about 500°C; under pressures from ambient to 500 psig; for periods of time from about 1 minute to about 100 hours; under conditions where the gas is stationary or moving; and under conditions were the impregnated catalyst support is stationary or moving. During the calcination step, the temperature is increased from ambient temperature in a controlled manner, preferably through a series of temperature increases followed by temperature hold periods. The calcining step may be carried out in any suitable calcining equipment, for example a rotary calciner or a belt conveyed calciner. [0021] In an embodiment, a KL-zeolite supported platinum aromatization catalyst is prepared by impregnating a KL-zeolite-support with tetramethylammonium chloride (TMAC), and/or tetramethylammonium fluoride (TMAF), and tetraamineplatinum chloride (TAPC); and calcinating the impregnated zeolite. In an embodiment, a KL-zeolite supported platinum aromatization catalyst is prepared by impregnating a KL-zeolite-support with ammonium fluoride, tetramethylammonium

chloride (TMAC), and tetraamineplatinum chloride (TAPC); and calcinating the impregnated zeolite.
[0022] In another aspect, the invention provides a process for reforming a hydrocarbon, for example aromatization, isomerization, dehydrogenation, and combinations thereof. For example, such a process could include contacting a hydrocarbon stream with a catalyst as described herein under suitable reaction conditions for aromatization of hydrocarbons, for example a temperature in the range of about 800° F to about 1050° F. In an embodiment, hydrogen is recovered as a product from the reforming process. In an embodiment, the catalyst comprises a composition made according to one of the methods described herein. [0023] In some embodiments, it may be desirable to provide a catalyst having less than about 1.3 wt% chlorine, alternatively less thpn about 1.0 wt% chlorine, alternatively less than about 0.5 wt% chlorine. In other embodiments, it may be desirable to provide a catalyst having less than about 1.3 wt% fluorine, alternatively less than about 1.0 wt% fluorine, alternatively less than about 0.5 wt% fluorine. Similarly, in other embodiments, it may be desirable to provide a catalyst having less than about 1.0 wt% platinum, alternatively less than about 0.6 wt% platinum, alternatively from about 0.2 to about 0.7 wt% platinum. In various embodiments, the atomic ratio of Pt : F : Cl in the catalyst is from about 1-0.5 : 3.3-1.7 : 10-5, respectively. As an example, the amount of fluorine, chlorine, and/or platinum in the catalyst can be controlled by controlling the amount of the respective precursors in the impregnation treatment.
[0024] In various embodiments, the catalyst composition comprises less than or equal to about 1 wt% platinum and has a Teo temperature of less than about 960°F and/or a deactivation rate of less than about 2.4 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.5 °F/day.
[0025] In various embodiments, the catalyst composition comprises less than or equal to about 0.5 wt% platinum and has a T6o temperature of less than about 1010°F and/or a deactivation rate of less than about 36 °F/day, alternatively a T60 temperature of less than about 965°F and/or a deactivation rate of less than about 3.5 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.2 °F/day.

1 I
[0026] In various embodiments, the catalyst composition comprises less than or equal to about 0.3 wt% platinum and has a T6o temperature of less than about 972°F and/or a deactivation rate of less than about 11.4 °F/day, alternatively a T6o temperature of less than about 950°F and/or a deactivation rate of less than about 1.5 °F/day, alternatively a T6o temperature of less than about 935°F and/or a deactivation rate of less than about 1.2 °F/day. The T60 temperature is defined as the temperature for a given feedstock at which the sum of the benzene wt% and toluene wt% in the reactor effluent is 60 wt%. Once this conversion rate is achieved at T6o, the deactivation rate is defined as a degree increase in temperature per day to maintain this conversion rate.
EXAMPLES
[0027] In each of the following examples, the prepared catalysts were ground, sieved to 20-40 mesh, and placed in a reactor comprising a metal reactor vessel in a temperature controlled furnace. After reducing the catalyst under flowing hydrogen, a feed stream of aliphatic hydrocarbon and hydrogen was introduced to the reactor vessel at a feed rate of 22mL/min and a pressure of 50 psig to obtain performance data. The reactor effluent composition was analyzed by gas chromatography to indicate the amount of benzene and toluene.
[0028] The catalysts prepared in accordance with Examples 1-11 below illustrate effects of varying the amount of platinum impregnated into the KL-zeolite catalyst when compared to Aromax® II catalyst. Under the present invention, significantly lower T6o values and deactivation rates can be obtained by preparing KL supported Pt zeolite catalysts using TMAF in place of NH4F and using a tetraalkylammonium chloride in place of NH4CI. The results are summarized in Table 1.
Example 1
[0029] A platinum-impregnated KL-zeolite catalyst containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.45g TMAF, 0.1 Og TMAC and 2.50g water is formed and added to a container containing 5.0g of a silica bound KL-zeolite extrudates that has been calcined for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp

rate is 0.25°C/min). The resultant catalyst contains 1.07 wt% Pt, 1.02 wt% Cl and 1.0 wt% F.
Example 2 (comparison)
[0030] A platinum-impregnated KL-zeolite catalyst containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.1 Og NH4F, and 0.05g NH4CI is formed and added to a container containing 5.0g of a silica bound KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp rate is 0.25°C/min). The resulting catalyst contains 0.55 wt% Pt, 0.5 wt% Cl and 1.0 wt% F.
Example 3
[0031] A platinum-impregnated KL-zeolite catalyst containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.1 Og TMAC and 2.50g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C (ramp rate is 0.5°C/min) and then calcined at 300°C for another 2 hours (ramp rate is 0.25°C/min). The resulting catalyst contains 0.54 wt% Pt, 0.83 wt% Cl and 1.0 wt% F.
Example 4 (comparison)
[0032] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.40g NH4F, and 0.8g NH4CI (0.8% aqueous solution) is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours ambient temperature. The impregnated KL-zeolite is dried in a vacuum for four hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.34 wt% Cl and 1.1 wt% F.
Example 5
[0033] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 0.40g NH4F, and 0.14g TMAC is formed and added to a container containing 18.23g of a

I t
KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours ambient temperature. The impregnated KL-zeolite is dried in a vacuum for four hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cland1.12wt%F.
Example 6
[0034] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.78g TMAF, 0.1 Og TMAC and 6.90g water is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.30 wt% Cl and 1.12 wt% F.
Example 7
[0035] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.84g TMAF, and 7g NH4CI is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.31 wt% Cl and 1.15 wt% F.
Example 8
[0036] A platinum-impregnated KL-zeolite catalyst containing 0.29 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1g TAPC, 1.60g TMAF and 0.11g TMAC is formed and added to a container containing 18.22g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.29 wt% Pt, 0.30 wt% Cl and 1.00 wt% F.

[0037] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 2.05g TMAF and 0.1 Og TMAC is formed and added to a container containing 18.25g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30,wt% Pt, 0.30 wt% Cl and 1.28 wt% F.
Example 10
[0038] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.75g TMAF, 0.18g tetraethylammonium chloride (TEAC) and 6.50g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cl and 1.09 wt% F.
Example 11
[0039] A platinum-impregnated KL-zeolite catalyst containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.75g TMAF, 0.30g tetrabutylammonium chloride (TBAC) and 6.50g water is formed and added to a container containing 18.29g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for 2 hours. The resulting catalyst contains 0.30 wt% Pt, 0.32 wt% Cl and 1.09 wt% F.

* Temperature (°F) at which the sum of the benzene wt% and toluene wt% in the reactor effluent is 60 wt%.
[0040] The results in Table 1 demonstrate that the substitution of TMAF and TMAC for NH4F and NH4CI, respectively, significantly decreases the deactivation rate and/or the T6o value. Example 1 used an impregnation comprising TAPC, TMAC and TMAF and produced a 1.0 wt% Pt. When compared to the Aromax® II catalyst, there was a 24° F reduction in the T6o value. By reducing the amount of platinum from 1.0 wt% to 0.5 wt%, as shown in the comparison of Examples 2 and 3, the catalyst made using TAPC, NH4F and NH4CI (Example 2) had a 75° F increase in the T6o value and a significant increase in the deactivation rate when compared to the Aromax® II catalyst which contained 1 wt% platinum.
[0041] While the catalyst containing 0.5 wt% platinum made by using TAPC, TMAF and TMAC (Example 3) did not show improvement over the Aromax® II catalyst with respect to the T6o value or the deactivation rate, the catalyst was a significant improvement over Example 2 which is an Aromax® II type catalyst, but containing 0.5 wt% platinum.
[0042] Examples 4 and 6 show the differences between Aromax® II catalyst and an Aromax® II type catalyst containing 0.3 wt% platinum and a catalyst prepared using TAPC, TMAF and TMAC containing 0.3 wt% platinum. The Aromax® II type catalyst (Example 4) showed a significant increase in the T6o value and in the deactivation rate when compared to the Aromax® II catalyst (comparison) and a platinum-impregnated KL-zeolite catalyst of the invention made in accordance with
Example 6.
[0043] Example 4 and 5 show the differences between an Aromax® II type
catalyst containing 0.3 wt% platinum and a catalyst prepared using TAPC, NH4F,

and TMAC containing 0.3 wt% platinum. The Aromax® II type catalyst (Example 4)
showed a significant increase in the deactivation rate when compared to the
platinum-impregnated KL-zeolite catalyst of the invention made in accordance with
Example 5.
[0044] Examples 7-11 show improved T6o values and lower deactivation rates
than comparative Example 4 when TMAF was substituted for NH4F. Examples 8
and 9 show the effects of fluorine and chlorine loading, as shown in more detail
below.
10045] Examples 3, 12, 13, and 14 in Table 2 illustrate effects on T6o value
and the deactivation rate when the amount of chlorine in the catalyst is varied.
Examples 12,13, and 14 were prepared as follows:
Example 12
[0046] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.02g TMAC and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.
Example 13
[0047] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, 0.05g TMAC and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.
Example 14
[0048] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.45g TMAF, and 2.0g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed

to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.

[0049] Table 2 is a comparison of changes in the chlorine content of catalyst prepared using TAPC, TMAF and TMAC. The results demonstrate a progressively lower deactivation rate and T6o value as chlorine levels are reduced. Example 2 demonstrates that a poor T6o value and deactivation rate are obtained when the impregnate comprises NH4F and NH4CI instead of TMAF and TMAC. [0050] Examples 15-23 (in addition to Examples 6-11) set forth procedures for preparing KL supported Pt zeolite aromatization catalysts containing about 0.3 wt% platinum. The catalysts produced have varying amounts of fluorine and chlorine.
Example 15
[0051] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.08g TMAF and 4.5g water is formed and added to a container containing 9.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 16
[0052] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.16g TAPC, 2.55g TMAF, 8.0g TMAC and 7.0g water is formed and added to a container containing 29.50g of a KL-

zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 17
[0053] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.1 Og TAPC, 1.28g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 18
[0054] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.60g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 68 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 19
[0055] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.80g TMAF, 0.049g TMAC and 4.5g water is formed and added to a container containing 9.26g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 20
[0056] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.78g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.23g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite

and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 21
[0057] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.92g TMAF, 0.07g TMAC and 7.0g water is formed and added to a container containing 18.24g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 22
[0058] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.50g TAPC, 0.82g TMAF, 0.06g TMAC and 4.0g water is formed and added to a container containing 9.11g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 23
[0059] A platinum KL-zeolite containing 0.3 wt% platinum is prepared in the following manner. An impregnating mixture of 0.05g TAPC, 0.82g TMAF, 0.1 Og TMAC and 4.0g water is formed and added to a container containing 9.11g of a KL-zeolite that has been baked for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
[0060] The Tw and deactivation rate data for the catalysts prepared in accordance with Examples 15 - 23 as well as Examples 6-11 are summarized in Table 3.

1
[0061] The results of Table 3 show that satisfactory T6o values and low deactivation rates can be obtained from a low-platinum load catalyst formed by using the TAPC, TMAF and TMAC impregnate (Examples 16-23) to prepare the catalyst on a KL-zeolite support. The results show further that when TMAF is used in place of NH4F, the catalyst has lower T^ values and lower deactivation rates than catalysts containing 0.3 wt.% and 0.5 wt.% platinum prepared using an impregnate containing TAPC, NH4F and NH4CI. See comparative Examples 2 and 4 in Table 1. [0062] Table 4 is a comparison of changes in the fluorine impregnating agent used to prepare the catalyst.
Example 24
[0063] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC and 4.5g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 75°C and then 2 hours at 170°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.

Example 25
[0064] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.1 Og ammonium chloride and 4.8g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 10 hours at 95°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 160°C and then calcined at 300°C for another 2 hours.
Example 26
[0065] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.20g TMAC and 4.8g water is formed and added to a container containing 10.Og of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 95°C, and then 2 hours at 160°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.
Example 27
[0066] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.20g TAPC, 0.15g ammonium chloride, 0.2g ammonium fluoride and 4.5g water is formed and added to a container containing 10.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at 70°C. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 300°C for another 2 hours.
Example 28
[0067] A platinum KL-zeolite containing 1.0 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 0.1g ammonium fluoride, 0.1 Og TMAC and 2.4g water is formed and added to a container containing 5.0g of a KL-zeolite predried for 2 hours at 538°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 20 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
[0068] The T6o and deactivation rate data for the catalysts prepared in accordance with Examples 24 - 28 is summarized in Table 4.

[0069] The results of Table 4 show that satisfactory T6o values and low deactivation rates can be obtained by using a TAPC, TMAC and ammonium fluoride impregnate to prepare the catalyst on a KL-zeolite support (Example 28). Conversely, where no fluorine impregnate was used (Examples 24-26), or where ammonium fluoride was used in conjunction with ammonium chloride (Example 27), the resulting T6oand deactivation rates were undesirably higher. [0070] In addition to the methods described in the Examples above, the catalysts of the present invention can be prepared by impregnating a suitable catalytic substrate with TAPC with hydrogen fluoride (HF), hydrogen chloride (HCI) and an organic or inorganic hydroxide represented by the formula N(R)4OH, where R represents hydrogen or a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms.
Example 29
[0071] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI, 0.83g ammonium hydroxide and 2.0g water is formed and added to a container containing 10.97g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 30
[0072] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI, 2.45g tetramethylammonium hydroxide and 0.50g water is formed and added to a container containing 10.96g of a KL-zeolite predried for 2 hours at 250°C. The

mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 31
[0073] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI and 2.8g tetraethylammonium hydroxide is formed and added to a container containing 10.96g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
Example 32
[0074] A platinum KL-zeolite containing 0.5 wt% platinum is prepared in the following manner. An impregnating mixture of 0.10g TAPC, 1.50g HF, 0.64g HCI and 6.8g tetrapropylammonium hydroxide is formed and added to a container containing 10.93g of a KL-zeolite predried for 2 hours at 250°C. The mixture is impregnated into the KL-zeolite and then allowed to stand for 16 hours at ambient temperature. The impregnated KL-zeolite is dried in a vacuum for 2 hours at 170°C and then calcined at 350°C for another 2 hours.
[0075] The results of Examples 29-32 are summarized in Table 5. This table shows that low loading catalysts containing 0.5 wt% platinum, 1.03 wt% fluorine and 0.39 wt% chlorine prepared using TAPC, HF, HCI and ammonium hydroxide or a tetraalkylammonium hydroxide result in low fouling rates.

reactor effluent is 60 wt%.
[0076] While the foregoing discussion is intended to provide a detailed illustration of certain embodiments of the invention, it will be appreciated that additional

embodiments are also possible under the claims provided herein. It will also be appreciated that numerical values and ranges are presented in approximate form such that small or inconsequential deviations from such values are intended to be within the scope of the values and ranges presented.

CLAIMS
The following is claimed:
1. A method of making a catalyst composition, comprising:
impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor.
2. The method of claim 1 wherein the ammonium halide precursor is represented by
the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted
carbon chain molecule having 1-20 carbon atoms wherein each R may be the
same or different.
3. The method of claim 2 wherein the large pore zeolite is an L-type zeolite.
4. The method of claim 2 wherein the large pore zeolite is a potassium L-type zeolite.
5. The method of claim 2 wherein R is an alkyl.
6. The method of claim 2 wherein R is selected from the group consisting of methyl,
ethyl, propyl, butyl, and combinations thereof.
7. The method of claim 2 wherein R is methyl.
8. The method of claim 2 wherein X is selected from the group consisting of F, Cl, Br,
I, and combinations thereof.
9. The method of claim 6 wherein X is selected from the group consisting of F, Cl, Br,
I, and combinations thereof.
10. The method of claim 2 wherein X is F.
11. The method of claim 2 wherein X is Cl.
12. The method of claim 2 wherein the halide precursor is tetramethylammonium
chloride.
13. The method of claim 2 wherein the halide precursor is tetramethylammonium
fluoride.
14. The method of claim 12 wherein the halide precursor further comprises
tetramethylammonium fluoride.
15. The method of claim 2 wherein the halide precursor further comprises ammonium
chloride.
16. The method of claim 12 wherein the halide precursor further comprises ammonium
chloride.

17. The method of claim 13 wherein the halide precursor further comprises ammonium
chloride.
18. The method of claim 14 wherein the halide precursor further comprises ammonium
chloride.
19. The method of claim 2 wherein the halide precursor further comprises ammonium
fluoride.
20. The method of claim 12 wherein the halide precursor further comprises ammonium
fluoride.
21. The method of claim 13 wherein the halide precursor further comprises ammonium
fluoride.
22. The method of claim 14 wherein the halide precursor further comprises ammonium
fluoride.
23. The method of claim 15 wherein the halide precursor further comprises ammonium
fluoride.
24. The method of claim 16 wherein the halide precursor further comprises ammonium
fluoride.
25. The method of claim 17 wherein the halide precursor further comprises ammonium
fluoride.
26. The method of claim 18 wherein the halide precursor further comprises ammonium
fluoride.
27. The method of claim 2, wherein the platinum precursor is selected from the group
consisting of ammonium tetrachloroplatinate, chloroplatinic acid,
diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum
(II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride,
tetraammineplatinum (II) hydroxide, tetraammineplatinum (II) nitrate, and
combinations thereof.
28. The method of claim 2 wherein the platinum precursor is tetraamineplatinum
chloride.
29. The method of claim 12 wherein the platinum precursor is tetraamineplatinum
chloride.

30. The method of claim 13 wherein the platinum precursor is tetraamineplatinum
chloride.
31. The method of claim 14 wherein the platinum precursor is tetraamineplatinum
chloride.
32. The method of claim 16 wherein the platinum precursor is tetraamineplatinum
chloride.
33. The method of claim 17 wherein the platinum precursor is tetraamineplatinum
chloride.
34. The method of claim 18 wherein the platinum precursor is tetraamineplatinum
chloride.
35. The method of claim 20 wherein the platinum precursor is tetraamineplatinum
chloride.
36. The method of claim 21 wherein the platinum precursor is tetraamineplatinum
chloride.
37. The method of claim 22 wherein the platinum precursor is tetraamineplatinum
chloride.
38. The method of claim 23 wherein the platinum precursor is tetraamineplatinum
chloride.
39. The method of claim 24 wherein the platinum precursor is tetraamineplatinum
chloride.
40. The method of claim 25 wherein the platinum precursor is tetraamineplatinum
chloride.
41. The method of claim 26 wherein the platinum precursor is tetraamineplatinum
chloride.
42. The method of claim 1 wherein the ammonium halide precursor comprises at least
one acid halide and at least one ammonium hydroxide represented by the formula
N(R')4OH, where R1 is hydrogen or a substituted or unsubstituted carbon chain
molecule having 1-20 carbon atoms wherein each R' may be the same or different.
43. The method of claim 42 wherein the large pore zeolite is an L-type zeolite.
44. The method of claim 42 wherein the large pore zeolite is a potassium L-type
zeolite.

45. The method of claim 42 wherein R* is an alkyl.
46. The method of claim 42 wherein R' is selected from the group consisting of methyl,
ethyl, propyl, butyl, and combinations thereof,
47. The method of claim 42 wherein R1 is methyl.
48. The method of claim 42 wherein the acid halide is HCI, HF, HBr, HI, or
combinations thereof.
49. The method of claim 46 wherein the acid halide is HCI, HF, or both.
50. The method of claim 47 wherein the acid halide is HCI.
51. The method of claim 47 wherein the acid halide is HF.
52. The method of claim 42 wherein the halide precursor further comprises ammonium
chloride, ammonium fluoride, or both.
53. The method of claim 49 wherein the halide precursor further comprises ammonium
chloride, ammonium fluoride, or both.
54. The method of claim 43 wherein the platinum precursor is selected from the group
consisting of ammonium tetrachloroplatinate, chloroplatinic acid,
diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum
(II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride,
tetraammineplatinum (II) hydroxide, tetraammineplatinum (II) nitrate, and
combinations thereof.
55. The method of claim 42 wherein the platinum precursor is tetraamineplatinum
chloride.
56. The method of claim 48 wherein the platinum precursor Is tetraamineplatinum
chloride.
57. The method of claim 49 wherein the platinum precursor is tetraamineplatinum
chloride.
58. The method of claim 50 wherein the platinum precursor is tetraamineplatinum
chloride.
59. The method of claim 51 wherein the platinum precursor is tetraamineplatinum
chloride.
60. The method of claim 53 wherein the platinum precursor is tetraamineplatinum
chloride.

61. The method of claim 2 wherein the ammonium halide precursor further comprises
at least one acid halide and at least one ammonium hydroxide represented by the
formula N(RI)4OH, where R1 is hydrogen or a substituted or unsubstituted carbon
chain molecule having 1-20 carbon atoms wherein each R1 may be the same or
different.
62. The method of claim 61 wherein the large pore zeolite is a potassium L-type
zeolite.
63. The method of claim 61 wherein each R and R1 are selected from the group
consisting of methyl, ethyl, propyl, butyl, and combinations thereof.
64. The method of claim 61 wherein X is selected from the group consisting of F, Cl,
Br, I, and combinations thereof.
65. The method of claim 61 wherein the acid halide is HCI, HF, or both.
66. The method of claim 61 wherein the halide precursor further comprises ammonium
chloride, ammonium fluoride, or both.
67. The method of claim 61 wherein the platinum precursor is selected from the group
consisting of ammonium tetrachlorop latin ate, chloroplatinic acid,
diammineplatinum (II) nitrite, bis (ethylenediamine)platinum (II) chloride, platinum
(II) acetylacetonate, dichlorodiammine platinum, platinum (II) chloride,
tetraammineplatinum (II) hydroxide, tetraammineplatinum chloride,
tetraammineplatinum (II) nitrate, and combinations thereof.
68. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt%
chlorine.
69. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt%
chlorine.
70. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt%
fluorine.
71. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt%
fluorine.
72. The method of claim 2, wherein the catalyst comprises less than about 1.3 wt%
chlorine and less than about 1.3 wt% fluorine.

73. The method of claim 42, wherein the catalyst comprises less than about 1.3 wt%
chlorine and less than about 1.3 wt% fluorine.
74. The method of claim 2, wherein the catalyst comprises platinum in the range of
about 0.2 wt% to about 0.7 wt%.
75. The method of claim 42, wherein the catalyst comprises platinum in the range of
about 0.2 wt% to about 0.7 wt%.
76. The method of claim 2, wherein the catalyst comprises less than about 0.6 wt%
platinum, less than about 1.3 wt% chlorine, and less than about 1.3 wt% fluorine.
77. The method of claim 42, wherein the catalyst comprises less than about 0.6 wt%
platinum, less than about 1.3 wt% chlorine, and less than about 1.3 wt% fluorine.
78. The process of claim 1 wherein the catalyst has a deactivation rate of less than
about 2.4 °F/day and a T6o of about 875 to about 975 °F.
79. The process of claim 2 wherein the catalyst has a deactivation rate of less than
about 2.4 °F/day and a T6o of about 875 to about 975 °F.
80. The process of claim 42 wherein the catalyst has a deactivation rate of less than
about 2.4 °F/day and a T6o of about 875 to about 975 °F.
81. The process of claim 61 wherein the catalyst has a deactivation rate of less than
about 2.4 °F/day and a T6o of about 875 to about 975 °F.
82. A method of making a catalyst composition, comprising:
impregnating a large pore zeolite support with a platinum precursor; at least one acid halide; and at least one organic ammonium hydroxide represented by the formula NfR'^OH, where R' is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R' may be the same or different.
83. A method of making a catalyst composition, comprising:
impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor represented by the formula N(R)4X, where X is a halide and R is a substituted or unsubstituted carbon chain molecule having 1-20 carbon atoms wherein each R may be the same or different.
84. A composition made according to the method of claim 1.
85. A process for reforming a hydrocarbon, comprising:

contacting hydrocarbons with a catalyst under suitable reaction conditions for aromatizing the hydrocarbons, wherein the catalyst is formed by a process comprising impregnating a large pore zeolite support with a platinum precursor and at least one organic ammonium halide precursor.
86. The process of claim 85 wherein the catalyst has a deactivation rate of less than
about 2.4 °F/day and a T6o of about 875 to about 975 °F.
87. The process of claim 85 further comprising recovering hydrogen.
88. The process of claim 82 further comprising vacuum drying the impregnated
catalyst support.
89. The process of claim 83 further comprising vacuum drying the impregnated
catalyst support.
90. The process of claim 82 further comprising calcining the impregnated catalyst
support in air having a diluted oxygen content.
91. The process of claim 83 further comprising calcining the impregnated catalyst
support in air having a diluted oxygen content.
92. The process of claim 88 further comprising calcining the impregnated catalyst
support in air having a diluted oxygen content.
93. The process of claim 89 further comprising calcining the impregnated catalyst
support in air having a diluted oxygen content.

Documents:

3433-CHENP-2005 CLAIMS.pdf

3433-CHENP-2005 CORRESPONDENCE OTHERS.pdf

3433-CHENP-2005 CORRESPONDENCE PO.pdf

3433-chenp-2005-abstract.pdf

3433-chenp-2005-assignement.pdf

3433-chenp-2005-claims.pdf

3433-chenp-2005-correspondnece-others.pdf

3433-chenp-2005-description(complete).pdf

3433-chenp-2005-form 1.pdf

3433-chenp-2005-form 18.pdf

3433-chenp-2005-form 26.pdf

3433-chenp-2005-form 3.pdf

3433-chenp-2005-form 5.pdf

3433-chenp-2005-pct.pdf

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Patent Number

234558

Indian Patent Application Number

3433/CHENP/2005

PG Journal Number

29/2009

Publication Date

17-Jul-2009

Grant Date

08-Jun-2009

Date of Filing

16-Dec-2005

Name of Patentee

CHEVRON PHILLIPS CHEMICAL COMPANY LP

Applicant Address

10001 SIX PINES DRIVE THE WOODLANDS TEXAS 77380

Inventors:

#	Inventor's Name	Inventor's Address
1	WU, AN-HSIANG	4723 BROOK SHADOW DRIVE KINGWOOD TEXAS 77345

PCT International Classification Number

B01J 29/62

PCT International Application Number

PCT/US04/14848

PCT International Filing date

2004-05-12

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	10/464,195	2003-06-18	U.S.A.