Hydrocarbon conversion using group VIII metal/alumina catalysts activated with halosilane

Abstract

A catalyst comprising a Group VIII metal selected from platinum, iridium, osmium, palladium, rhodium, and ruthenium supported on alumina is activated at an elevated temperature with a halosilane such as silicon tetrachloride. In a preferred embodiment, hydrogen is used in conjunction with the halosilane. In another preferred embodiment HCl is used in conjunction with the halosilane. The resulting catalysts exhibit an outstandingly high isomerization rate constant in the isomerization of feedstocks such as normal butane to isobutane. The catalysts are also well suited for hydrocracking.

Description

BACKGROUND OF THE INVENTION

This invention relates to activating catalysts of selected Group VIII metals on alumina.

Platinum supported on alumina has long been used as an isomerization catalyst. It is broadly known to treat such materials with halogens to activate same. However, it has been found that the effectiveness of such treatments can vary widely and are not at all predictable.

SUMMARY OF THE INVENTION

It is an object of this invention to provide a hydrocarbon conversion catalyst of improved activity;

IT IS A FURTHER OBJECT OF THIS INVENTION TO PROVIDE A PROCESS FOR ACTIVATING A PLATINUM GROUP METAL/ALUMINA CATALYST UTILIZING A HALOSILANE;

IT IS A FURTHER OBJECT OF THIS INVENTION TO PROVIDE A PLATINUM GROUP METAL/ALUMINA CATALYST WHICH IS APPLICABLE TO COMMERCIAL SCALE OPERATIONS; AND

IT IS YET A FURTHER OBJECT OF THIS INVENTION TO PROVIDE A CATALYST CAPABLE OF EFFECTING ISOMERIZATION AT A HIGHER RATE CONSTANT.

In accordance with this invention, a catalyst of platinum, iridium, osmium, palladium, rhodium, and ruthenium on alumina is activated in the presence of a halosilane selected from chlorosilanes and bromosilanes at a temperature of greater than 1200.degree. F.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The catalysts which are activated in accordance with this invention are basically a selected Group VIII metal supported on an active alumina base. The applicable Group VIII metals are at least one of platinum, iridium, osmium, palladium, rhodium, and ruthenium. This class of catalysts is well-known in the prior art and generally contains from 0.01 to 10, preferably 0.1 to 1, weight percent metal based on the total catalyst weight including the alumina base. The preferred metal is platinum. These catalysts can also contain minor amounts of a halogen incorporated during preparation of the catalyst, chlorine and/or fluorine being the two halogens commonly present. Although one or both of these halogens can be present in the catalyst prior to activation by the process of the present invention, the catalyst containing them is not the equivalent of a catalyst which has been activated by the present process. The amount of halogen in the catalyst as prepared (i.e., prior to activation in accordance with this invention) if any, is usually less than about 1.5 weight percent based on the total weight of the catalyst.

To produce these catalysts, an alumina, well-known in the art as an "active" alumina is essential. Active aluminas may be synthetically prepared as by calcination of alumina gels which are formed by adding such reagents as ammonium hydroxide to a salt of aluminum, such as aluminum chloride or aluminum nitrate. These aluminas are generally gamma or eta aluminas depending upon the dehydrating conditions used. Similar active aluminas may be prepared by calcination of naturally occurring aluminas such as the monohydrate and the trihydrate. Bauxite is a common source of active alumina when properly calcined and dehydrated. The alumina base of the catalyst may contain minor amounts of silica and boron oxide. The amounts of these materials should be less than about 30 percent, preferably less than about 10 weight percent of the catalyst base component to produce the most active catalyst.

The halosilane is preferably a chlorosilane, which can be represented by the formula SiX.sub.4 in which each X can be the same or different and where at least one X is chlorine and the other X substituents are selected from the group consisting of hydrogen, chlorine and alkyl radicals containing from 1 to 3 carbon atoms per molecule. Exemplary compounds include silicon tetrachloride, trichlorosilane, monochlorosilane, trichloromethylsilane, dichloropropylsilane and the like. A presently preferred compound based on cost and availability is silicon tetrachloride. The corresponding bromosilanes can also be used.

When a hydrogen halide is used in the activating gas along with a halosilane, it is preferred that the halogens in each compound be the same. That is a combination consisting of silicon tetrachloride and hydrogen chloride is preferred rather than silicon tetrachloride and hydrogen bromide, for example.

While it is broadly known to activate platinum/alumina catalysts utilizing a halosilane in the presence of air at a relatively low temperature, it has surprisingly been discovered that activation in the absence of air utilizing a halosilane at a temperature above 1200.degree. F., preferably a temperature within the range of 1250.degree. to 1600.degree. F., more preferably a temperature within the range of 1250.degree. to 1450.degree. F. gives a superior catalyst. The air is preferably excluded during the activation of the catalyst to minimize crystal growth of the platinum component which otherwise tends to reduce the effectiveness of the catalyst. Indeed, if the catalyst of this invention is cooled from activation temperature down to 200.degree. to 1000.degree. F. in the presence of a halosilane, the activity of the catalyst is diminished.

The Pt, Ir, Os, Ru, Rh, or Pd metal on aluminum catalyst is first calcined in a manner known in the art, for instance, by heating to a temperature within the range of 500-900, more preferably 700.degree.-900.degree. F. for a time within the range of 1-10, preferably 1-3 hours. Preferably this is carried out in the presence of air although air is not essential.

The catalyst is then heated to the activation temperature in accordance with this invention of greater than 1200.degree. F., preferably 1250.degree.-1600.degree. F., more preferably 1250.degree.-1450.degree. F. This can be done in either a pure nitrogen atmosphere, a pure hydrogen atmosphere, or in a mixture of nitrogen and hydrogen. Hydrogen is preferred in the sense that excellent results can be obtained in a pure hydrogen atmosphere; however the initial heating from ambient temperature to activation temperature can be carried out in a mixture of hydrogen and nitrogen with essentially the same results as in pure hydrogen and with a cost saving in view of the fact that nitrogen is less expensive. Anhydrous HCl could also be present but it is not required.

The catalyst is then held at this temperature of greater than 1200.degree. F., preferably 1250.degree.-1600.degree. F., more preferably 1250.degree.-1450.degree. F. for a time of at least 10 minutes preferably at least one hour. A range of 1.0 to 15 hours, more preferably 1.5 to 5 hours is satisfactory. It is highly preferred during this holding at activation temperature that the atmosphere be hydrogen.

The catalyst is then treated with a dry activating gas comprising the halosilane while at said temperature of greater than 1200.degree. F., preferably 1250.degree.-1600.degree. F., more preferably 1250.degree.-1450.degree. F. for a time within the range of 1/10 to 10, preferably 1 to 3 hours. The atmosphere in the reaction chamber is preferably hydrogen. A mixture of hydrogen and anhydrous hydrogen chloride is also quite satisfactory. This is preferably done in the absence of nitrogen, preferably in the absence of both oxygen and nitrogen (i.e., in the absence of air) since both oxygen and nitrogen have a deleterious effect on the catalyst at this point. One convenient method of contacting the catalyst with the halosilane is to utilize a stream of hydrogen carrier gas which stream is divided and 2-20, preferably 5-15 volume percent of the hydrogen is passed through a saturator (a means for bubbling the hydrogen through liquid halosilane) so as to pick up some of the halosilane. Alternatively the halosilane can simply be metered into the hydrogen stream or directly into the zone containing the catalyst. The amount of halosilane in the hydrogen carrier gas will generally be within the range of 0.1 to 20, preferably 1 to 2 mole percent although this can vary greatly depending on the flow rate, the essential feature being the total amount of halosilane introduced. The streams are then combined and the combined stream passed over the catalyst.

The halosilane is contacted with the catalyst in an amount effective to impart a halide content to the catalyst and to increase the activity of the catalyst. In most instances some halide is already present. Generally the halide so added will range from 0.5 to 20, preferably 1 to 12, more preferably 5 to 8 weight percent calculated as the halide ion based on the weight of the catalyst. This is the amount brought into contact with the catalyst with about 80 percent thereof being actually incorporated into the catalyst until the catalyst approaches saturation. The amount of halogen calculated as halide ion actually incorporated by this treatment will generally be within the range of 1-10, preferably 2-6 weight percent halide ion based on the weight of the Pt, Ir, Os, Ru, Rh or Pd metal-alumina. If a saturator is used, the halosilane can be kept in a refrigerated condition either using a wet ice bath or a dry ice bath so as to maintain same in a liquid state where the halosilane has a boiling point below atmospheric temperature at the pressure used.

The thus activated catalyst is then cooled to ambient temperature. Preferably, this cooling is in a hydrogen or hydrogen-nitrogen atmosphere. In a more preferred embodiment, the catalyst is cooled from the above-noted activation temperature to a temperature of about 1100.degree. F. or below in pure hydrogen and thereafter cooled on to ambient temperature in an atmosphere containing both hydrogen and nitrogen. It is preferred that the hydrogen during the cooling from the activation temperature to the temperature of approximately 1100.degree. F. be passed over the catalyst at a relatively low rate, preferably not more than 0.15 to 0.45 liters per hour for each gram of catalyst until the catalyst is cooled to said temperature of about 1100.degree. F. Thereafter the hydrogen or hydrogen-nitrogen mixture can be passed over the catalyst at a higher rate, but still a rate generally not more than 1.1 to 3.0 liters per hour per gram of catalyst. It is to be noted that during the first portion of the cooling cycle the hydrogen is flowed through the catalyst mass and thus effectively purges most or all of the remaining halosilane. When a mixture of nitrogen and hydrogen are utilized during the heatup or during the cooling after the temperature has been reduced to 900.degree.-1200.degree. F., preferably 900.degree. to 1100.degree. F., the amount of nitrogen can vary from 1 to 99, preferably 5 to 97 mole percent based on the total moles of nitrogen and hydrogen. The procedure should be controlled so that the nitrogen content of the activated catalyst is below 200 parts per million, preferably below 50 parts per million.

Nitrogen can be tolerated without decreased catalyst activity during the entire cooling cycle if anhydrous hydrogen chloride is present. Thus, a cooling gas can comprise anhydrous hydrogen chloride, hydrogen, and nitrogen with nitrogen being the predominant constituent. A preferred ratio of hydrogen to HCl is from 0.5:1 to 2:1 with the nitrogen content being between 50 and 95 mole percent.

It is primarily with respect to long cooling periods such as are encountered in commercial scale operation that it is necessary to remove the halosilane prior to cooling below about 1000.degree. F., preferably before 1100.degree. F., more preferably before cooling below 1200.degree. F.

In an alternative embodiment a mass of said catalyst not yet activated and a separate mass of alumina containing no Group VIII platinum metal component are heated to said temperature of greater than 1200, preferably 1250-1600, more preferably 1250.degree.-1450.degree. F. and a stream of activating gas comprising halosilane and hydrogen is passed first through said alumina; the effluent stream from the bed of alumina is then passed directly to the mass of catalyst while still at said temperature of greater than 1200, preferably 1250-1600, more preferably 1250.degree.-1450.degree. F. One convenient method of doing this is simply to have a column packed with the catalyst and at the upstream end thereof a mass of alumina separated from the catalyst by means of quartz wool or the like. Relative amounts of alumina to catalyst can vary greatly, but will generally be within the range of 1 to 50 weight percent, preferably 10 to 30 weight percent alumina based on the total weight of alumina and catalyst.

In another alternate embodiment anhydrous hydrogen chloride can be present during the contacting of the catalyst with the halosilane. These two components can be present in over a wide range of portions. As noted hereinabove, the halosilane can be used alone (that is without any other halogen-containing compound) so the lower limit on the amount of anhydrous HCl is zero. The upper limit, however, can be as high as 90 to 99 percent, or stated in another way, the presence of only a small amount of halosilane in conjunction with anhydrous HCl results in production of an exceptionally effective catalyst.

The catalysts of the present invention are particularly applicable to the skeletal isomerization of isomerizable hydrocarbons including acyclic paraffins, and naphthenes. These catalysts are particularly suitable for the isomerization of straight chain or singly-branched paraffins containing four to eight carbon atoms per molecule including n-butane, n-pentane, n-heptane, methylpentane and the like. Some examples of naphthenes which can be isomerized with these catalysts and methylcyclopentane, dimethylcyclopentane, cyclohexane, methylcyclohexane, and the like. Actually these are equilibrium reactions as follows:

cyclohexane .revreaction. methylcyclopentane methylcyclohexane .revreaction. dimethylcyclopentane pentane .revreaction. methylbutane n-hexane .revreaction. methylpentanes .revreaction. dimethylbutanes

Conditions can be adjusted to give hydrocracking, as for instance to produce butane from n-octane.

The isomerization reaction conditions and recovery procedures can be varied to achieve the desired conversion in a manner known in the art. A presently preferred isomerization reaction is the isomerization of normal butane to isobutane.

Hydrocarbons to be isomerized are contacted with the activated catalysts prepared in accordance with the invention at an isomerization temperature of about 100.degree.-600.degree. F., more preferably 150.degree.-450.degree. F., in the presence of free hydrogen. The hydrogen-hydrocarbon mol ratios normally used during isomerization are within the range of about 0.25 to 10 to insure long catalyst life. Liquid hourly space velocities, i.e., the volume of liquid charge per hour per volume of catalyst, of about 0.1 to 15 are satisfactory and pressures within the range of atmospheric to 1500 psig in the isomerization zone are suitable.

Maintenance of catalyst activity during the isomerization process is aided by the inclusion of 0.001 to about 1 weight percent chloride in the feed in the form of chlorinated hydrocarbon promoters such as carbon tetrachloride, chloroform, ethyl chloride, isopropyl chloride, etc. This is not a substitute for the activation of the catalyst but it aids in maintaining over long process periods the high level of catalyst activity of the invention catalysts.

The isomerization process can be carried out either in a batchwise or continuous basis, preferably the latter. In a continuous process it is to be understood that hydrogen in the effluent product can be separated and recycled and that recycling of isomerization promoters, if employed, can be practiced.

These catalysts are also suitable for hydrocracking operations. Preferred process conditions for hydrocracking are as follows. Pressure: 50-5000 psig, preferably 100-3000 psig; temperature: 200.degree.-800.degree. F., preferably 300.degree.-700.degree. F.; liquid hourly space velocity: 0.1-30, preferably 0.5-20, and H.sub.2 /hydrocarbon mole ratio: 0.5-30, preferably 2-20. Applicable feeds include C.sub.5 and higher boiling hydrocarbons such as naphthas and distillates. The catalyst is especially useful in hydrocracking to produce C.sub.4 and lighter hydrocarbons. Feeds should be substantially free of poisons such as water, oxygen-containing organic compounds and sulfur compounds.

EXAMPLE I

A gamma-alumina in the form of 1/16 inch diameter extrudate was impregnated with an aqueous solution of chloroplatinic acid and hydrochloric acid sufficient to give a platinum content of 0.37 weight percent and a chloride content of 1.25 weight percent based on the calcined composite. The impregnated sample was dried in air at 240.degree. F. and calcined in air at 800.degree. F. for 2 hours. Six equal portions by weight were taken from the calcined catalyst and each portion was heated for two hours in a hydrogen atmosphere at the activation temperature to be used followed by activation in a silicon tetrachloride-hydrogen atmosphere at temperatures given in Table 1. After the heating period, each catalyst was removed from the furnace in its quartz tube, cooled in the activating ambient to about 200.degree. F. (12-13 minutes) and transferred to a reactor for testing. The isomerization tests were conducted at about 300.degree.-325.degree. F., at a space velocity of 4 parts liquid feed per part catalyst per hour (by volume, LHSV), 500 psig and a 0.5 hydrogen/feed mole ratio. The feed tested was n-butane containing about 200 ppm chloride as carbon tetrachloride. The results are presented in Table 1.

Table 1______________________________________Activation of Chlorided Alumina Platinum Catalyst InSilicon Tetrachloride-Hydrogen Atmosphere a) b) c)Run SiCl.sub.4 -H.sub.2 Wt. % Relative IsomerizationNo. Temp. .degree. F. Time, Hrs. SiCl.sub.4 Rate Constant at 315.degree. F.______________________________________1 1002 2.0 7.5 0.112 1200 2.0 7.9 1.013 1253 2.0 6.8 1.324 1355 1.8 6.5 1.795 1449 1.9 5.9 1.916 1548 2.0 4.7 1.91______________________________________ a) The H.sub.2 rate was 21 liters/hour (STP) during initial heating and 1 liters/hour during activation. Approximately 1 liter of the 11 liters/hou hydrogen gas was passed through SiCl.sub.4 to saturate it with the halide b) SiCl.sub.4 contacted with the catalyst based on calcined weight of the platinum-alumina. c) Calculated from the test results using the first order reversible reaction kinetic equations presented on pages 62-63 of "Chemical Reaction Engineering", Levenspiel, John Wiley & Sons, 1962, Library of Congress Catalog No. 62-15185.

The results show that the catalysts increase in activity with increasing activation temperature up to about 1450.degree. F. at which point the activity appears to be leveling out. Especially active catalysts are obtained at activation temperatures ranging from about 1250.degree. F. to about 1450.degree. F.

Because the cooling time was short it was possible to cool in the presence of the activating ambient. In a commercial scale operation where a longer cooling time (generally about 0.5 to 3 hours) would be required, it is highly preferred to purge any halosilane left from the catalyst with hydrogen prior to cooling.

EXAMPLE 2

Several runs were made to determine the effect of the amount of silicon tetrachloride added to the catalyst during the activating period on the isomerization activity of the resulting catalysts. Extruded gamma-alumina prills were impregnated with an aqueous solution of chloroplatinic acid and hydrochloric acid sufficient to impart a platinum content of 0.37 weight percent and a chloride content of 1.25 weight percent based on the calcined catalyst. The impregnated sample was dried and calcined in air a in the manner of Example 1. The calcined material was divided into portions of equal weight. Each portion was transferred to a quartz tube and heated at an elevated temperature in a silicon tetrachloride-hydrogen ambient and cooled following the procedure of Example 1. The feed tested was n-butane containing about 200 ppm chloride as carbon tetrachloride. The isomerization tests were conducted at 315.degree. F., a space velocit (LHSV) of 4,500 psig reaction pressure and a 0.5 hydrogen/feed mole ratio The results are presented in Table 2.

Table 2______________________________________Variation In Isomerization Activity Of CatalystWith Amount Of Silicon Tetrachloride______________________________________ Isomerization ResultsSiCl.sub.4 -H.sub.2 Isobutane in Relative.sup.b)Run Time, SiCl.sub.4.sup.a) C.sub.4 effluent RateNo. Temp. .degree. F. Hrs Wt. % Mole % Constant______________________________________7 1354 20.0 3.8 57.1 1.338 1355 1.8 6.5 61.5 1.79______________________________________ .sup.a) Based on calcined catalyst weight. .sup.b) Calculated as in Example 1.

The results show that more active catalysts are obtained when the amount of silicon tetrachloride used in activating the catalysts exceeds about 4 weight percent. Good results were obtained at 6.5 weight percent as the data demonstrate.

EXAMPLE 3

A platinum-alumina composite was prepared as described in Example 1 hereinabove. Portions of this composite were activated. Activation was carried out in a quartz tube in which a 37.0 gram portion of the platinum-alumina was placed in the tube below an 8.3 gram portion of alumina with quartz wool separating the two substances. The platinum-alumina was activated by heating for two hours in hydrogen alone at 1350.degree. F. followed by 2 hours in H.sub.2 -SiCl.sub.4 mixture containing 1.3- 1.5 mol percent SiCl.sub.4. Activated catalyst was cooled to about 200.degree. F. in 3 hours. With one portion, SiCl.sub.4 was stopped at the end of the 2-hour period at 1350.degree. F. With the second portion the SiCl.sub.4 addition was continued until the average catalyst temperature was 994.degree. F. With a third portion, the SiCl.sub.4 addition was continued until the average temperature was 582.degree. F. With a fourth portion, the SiCl.sub.4 addition was continued until the average temperature was about 200.degree. F.

Representative samples of these activated catalysts were tested for the isomerization of n-butane at 305.degree. F., four LHSV, 500 psig and with 0.5 H.sub.2 /butane mol ratio. Relative rate constants calculated from the test data show that stopping the SiCl.sub.4 addition at the end of the activation period gave much more active catalysts as is shown in Table 3.

Table III______________________________________Run No. 9 10 11 12______________________________________ActivationTemp., .degree. F. 1351 1352 1356 1354Time, hrs. 2.0 2.0 2.0 2.0H.sub.2, 1/hr. 11.5 11.3 11.3 11.3SiCl.sub.4, mol % in H.sub.2 -SiCl.sub.4 1.5 1.3 1.4 1.4CoolingTemp, SiCl.sub.4 stopped, .degree. F. 1354 994 582 .perspectiveto.200Time from activation 3.0 3.0 3.0 3.0temp. to .perspectiveto. 200.degree. F.H.sub.2, 1/hr 10.0 11.3 11.3 11.3 10.0.sup.a 10.0.sup.a 10.0.sup.aRelative Isomerization 1.65 1.01 0.85 0.89Rate constant at 305.degree. F.______________________________________ .sup.a H.sub.2 11.3 1/hr until SiCl.sub.4 stopped, then reduced to 10.0 1/hr. 10.0 1/hr equivalent to 4.3 cu ft/lb. of platinum-alumina.

These results show that when the cooling time is more than about 0.5 hours, the halosilane should not be present after the catalyst is cooled below activation temperature or at least below about 1100.degree. F.

EXAMPLE 4

A platinum-alumina composite was prepared as described in Example 1. Then this platinum-alumina composite was activated. Activation was carried out in a quartz tube in which a 4 foot portion of the platinum-alumina was placed in the tube below a 1 foot portion of alumina with quartz wool separating the two substances. This 4 foot portion was viewed as four sections of 1-foot each for the purpose of this test. The platinum-alumina was then activated as shown in Table IV hereinbelow and the resulting catalyst subjected to analysis. In addition the catalyst was utilized to isomerize n-butane in the same manner as in the above examples. No nitrogen was present in the preheating and cooling gas.

Table IV______________________________________Activation of 5 foot bed 13 activation tube packed with 1-ft. ofRun No. alumina.sup.2 above 4-ft of Pt-alumina.sup.a______________________________________Section of bed 1 2 3 4 5 Al.sub.2 O.sub.3 Pt-Al.sub.2 O.sub.3Weight, g 69.5 69.5 69.5 69.5 69.5Activation.sup.bTemp, .degree. F. 1342 1342 1355 1351 1354Time, hr. 2.0H.sub.2, 1/hr (SCFH/lbPt-Al.sub.2 O.sub.3) 88(5.1)SiCl.sub.4 in H.sub.2 -SiCl.sub.4,mol per cent 1.5SiCl.sub.4, wt % of Pt-al 7.5calculated as inExample ICooling1350 to 1100.degree. F.H.sub.2, 1/hr (SCFH/lb.Pt-Al.sub.2 O.sub.3) 77(4.4)Time, hrs. 1.81100 to .perspectiveto.300.degree. F.H.sub.2, 1/hr (SCFH/lb.Pt-Al.sub.2 O.sub.3) 380(22)Time, hrs. 2.6Activated CatalystPt, wt. % -- 0.38 0.36 0.39 0.37Cl, wt. % 2.13 3.60 3.57 3.74 3.78Si, wt. % 4.94 0.27 0.12 0.11 0.11Surface area, m.sup.2 /g 143 144 139 141 138Apparent Bulk Densityg/cc -- 0.71Nitrogen, ppm -- -- 1.1 -- --Isomerization Activity.sup.diC.sub.4 H.sub.10 in C.sub.4 effluent, -- 60.1 62.1 62.0 61.4Relative rate constant -- 1.54 1.80 1.78 1.70______________________________________ .sup.a Extruded alumina. .sup.b Catalysts preheated at .perspectiveto.1350.degree. F. for 2 hrs. i H.sub.2 before activation. .sup.c Gas rates at 32.degree. F. (60.degree. F. for SCFH) .sup.d Isomerization conditions: 305.degree. F., 4 LHSV, 500 psig, and 0. H.sub.2 /butane mole ratio.

These results show that catalysts of high activity can be produced by passing the halosilane activating agent into contact with an alumina bed and thereafter directly passing the effluent therefrom into contact with the catalyst.

EXAMPLE 5

Another platinum-alumina composite was prepared using a procedure involving holding the composite at 1300.degree. F. for over an hour before chloriding, and with no nitrogen being present during activation. The results are shown hereinbelow in Table V.

Table V______________________________________Run 14Section of Pt-Al.sub.2 O.sub.3 Bed.sup.a 1 2 4Preheating, R.T. to 1350 F.Time, hr. 2Gas Composition, mole %H.sub.2 3.5N.sub.2 96.5Total 100.0Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3.sup.b 10.0Period at 1350 F. before ChloridingTime, hr. 1.2Gas Composition, mole %H.sub.2 3.5N.sub.2 96.5Total 100.0Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3 10.0Chloride ActivationTemp. F. 1345 1348 1364Time, hr. 2.0H.sub.2, SCFH/lb Pt-Al.sub.2 O.sub.3 5.3N.sub.2, SCFH/lb Pt-Al.sub.2 O.sub.3 0.0SiCl.sub.4 in gas, mole % 1.57SiCl.sub.4, wt. % of Pt-Al.sub.2 O.sub.3 7.7Cooling1350 F. to 1100 F.Time, hr. 2.0Gas Composition, mole %H.sub.2 5N.sub.2 95Total 100Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3 4.81100 F. to 300 F.Time, hr. 2.4Gas Composition, mole %H.sub.2 5N.sub.2 95Total 100Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3 23Nitrogen in Activated Catalyst, ppm 211.sup.c 272 dIsomerization Activity.sup.eiC.sub.4 H.sub.10 in C.sub.4 H.sub.10 Effluent, Mole % 56.5 53.5 52Relative Rate Constant 1.26 1.09 1.01______________________________________ .sup.a Activation tube packed with 1-ft. of extruded alumina about 4-ft. of 0.35 Pt on alumina. .sup.b Gas rates at 60 F. .sup.c Nitrogen content of alumina section was 4 ppm. .sup.d Not shown. .sup.e Isomerization conditions: 305 F., 4 LHSV, 500 psig, and 0.5 H.sub. /butane mole ratio.

These data show that when nitrogen was present in all the preheating and cooling the catalyst contained over 200 ppm (wt.) nitrogen and the rate constant was lower.

EXAMPLE 6

In the following run a lower activity alumina was used than in Example 5 and thus all of the rate constants are lower than would have been the case with an identical alumina. This run does show, however, that nitrogen can be used when cooling from about 1100.degree. F. to about 250.degree. F., if it is avoided in cooling from 1350.degree. F. to 1100.degree. F. The run also shows that nitrogen can be used during the preheating when the catalyst is maintained in a hydrogen atmosphere for about one hour or longer before chloriding. The nitrogen content of the activated catalyst was only 4 ppm (wt.).

Table VI______________________________________Run 15Section of Pt-Al.sub.2 O.sub.3 Bed.sup.a 1 2 3 4Preheating, R.T. to 1350 F.Time, hr. 2.0Gas Composition, mole %H.sub.2 20N.sub.2 80Total 100Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3.sup.b 27.0Period at 1350 F. beforeChloriding Time, hr. 1.5Gas Composition, mole %H.sub.2 100Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3 5.4Chloride ActivationTemp, F. 1360 1373 1354 1341TIme, hr. 2.0H.sub.2, SCFH/lb Pt-Al.sub.2 O.sub.3 6.2SiCl.sub.4 in H.sub.2 -SiCl.sub.4, mole % 1.49SiCl.sub.4, wt % of Pt-Al.sub.2 O.sub.3 8.4Cooling1350 F. to 1100 F.Time, hr 2.0Gas Composition, mole %H.sub.2 100Gas Rate, SCFH/lb Pt-Al.sub.2 O.sub.3 5.41100 to 250 F.Time, hr. 2.6Gas Composition, mole %H.sub.2 20N.sub.2 80Total 100Gas Rate, SCFH/lb Pt-Al.sub.2 0.sub.3 27.0Activated CatalystPt. wt % 0.36 0.36 0.36 0.37Cl, wt % 3.25 3.44 3.67 3.82Si, wt % 0.70 0.10 0.09 0.10Surface Area, m.sup.2 /g 140 134 139 142Apparent Bulk Density,g/cc 0.62 0.62 0.62 0.62Nitrogen in ActivatedCatalyst, ppm 4.sup.c 4.sup.c 4.sup.c 4.sup.cIsomerization Activity.sup.diC.sub.4 H.sub.10 in C.sub.4 Effluent 49.3 59.7 58.8 58.5Relative Rate Constant 0.89 1.48 1.40 1.38______________________________________ .sup.a Activation tube packed with 1-ft of extruded alumina above 4-ft of 0.35 Pt on alumina. .sup.b Gas rates at 60 F. .sup.c Nitrogen content on a blend of this and a duplicate run. .sup.d Isomerization conditions: 305 F. 4 LHSV, 500 psig, and 0.5 H.sub.2 /butane mole ratio.

EXAMPLE 7

A gamma-alumina in the form of 1/16 inch diameter extrudate was impregnated with an aqueous solution of chloroplatinic acid and hydrochloric acid sufficient to give a platinum content of 0.37 weight percent and a chloride content of 1.25 weight percent based on the calcined composite. The impregnated sample was dried in air at 240.degree. F. and calcined in air at 800.degree. F. for 2 hours. Equal portions by weight were taken from the calcined catalyst and each portion was heated for two hours in a hydrogen atmosphere followed by activation at about 1250.degree. F. in the medium chosen for 2 hours as shown in the Table. After activation each catalyst was removed from the furnace in its quartz tube, cooled in the activating ambient to about 200.degree. F. (12-13 minutes) and transferred to a reactor for testing. The isomerization tests were conducted at about 305.degree.-325.degree. F. at a space velocity of 4 parts liquid feed per part catalyst per hour (by volume, LHSV), 500 psig and a 0.5 hydrogen/feed mole ratio. The feed tested was n-butane containing about 200 ppm chloride as carbon tetrachloride. The results are presented in the Table.

Table VII______________________________________Amount of SiCl.sub.4 Isomerization Results at 305-325.degree. F. Added to Activating Isobutanes in C.sub.4 Relative rateRun Gas Wt % of HCl.sup.(a) Effluent, Mole 9 Constant.sup.(b)______________________________________16 none 53.3 1.0917 1.2 58.0 1.4018 2.8 58.0 1.40______________________________________ .sup.(a) Unpromoted ambient consisted of 62 mole per cent HCl and 38 mole percent H.sub.2. The activation gas flow was 29 liters per hour at STP. The SiCl.sub.4 was added by passing a portion of the H.sub.2 through the silicon tetrachloride. .sup.(b) Calculated from the test results using the first order reversibl reaction kinetic equations presented on pages 62-63 of "Chemical Reaction Engineering" Levenspiel, John Wiley & Sons, 1962, Library of Congress Catalog No. 62-15185.

This shows the effect of silicon tetrahalides in combination with HCl, whereby an improved relative rate constant is achieved.

EXAMPLE 8

A gamma alumina in the form of 1/16 inch diameter extrudate was impregnated with an aqueous solution of chloroplatinic acid to give a platinum content of 0.35 weight percent based on the calcined composite. The impregnated sample was dried in air at 234.degree. F. and calcined in air at 800.degree. F. for 2 hours. A portion of this platinum-alumina was heated at about 1348.degree. F. for 1.5 hours in hydrogen and then in a silicon tetrachloride-hydrogen atmosphere containing 1.3 mole percent silicon tetrachloride for 2 hours. After the heating period, the catalyst in its quartz tube was removed from the furnace and cooled in the silicon tetrachloride-hydrogen gas to about 200.degree. F. in 13 minutes. During this activation, silicon tetrachloride equivalent to 8.3 weight percent of the platinum-alumina contacted the catalyst. The catalyst was then heated in hydrogen at 800.degree. F. for 5 hours, cooled, and a portion was transferred to a reactor for testing.

An isohexane feed containing 200-300 ppm (wt.) chloride as carbon tetrachloride was passed over the catalyst at about 275.degree. F., 900 psig, 3 LHSV, and 8 hydrogen/feed mole ratio for 20 hours in an isomerization test. Then the temperature was raised for hydrocracking tests. At 528.degree. F., the reactor hydrocarbon effluent had the following composition:

______________________________________Component Wt. %______________________________________Methane 2.5Ethane 3.0Propane 60.9Isobutane 11.1Normal Butane 9.8Isopentane 7.0Normal Pentane 2.8Pentene 0.6C.sub.6 + .sup.a 2.3 100.0______________________________________ .sup.a Predominantly hexane. As the data show, the hexane was almost completely hydrocracked.

While this invention has been described in detail for the purpose of illustration, it is not to be construed as limited thereby but is intended to cover all changes and modifications within the spirit and scope thereof.

Claims

1. A hydrocarbon skeletal isomerization process which comprises:

a. contacting an isomerizable hydrocarbon selected from the group consisting of acyclic paraffin and naphthene under isomerization conditions with a catalyst produced by (1) heating an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst to a temperature of greater than 1200.degree. F. in an atmosphere selected from the group consisting of nitrogen, hydrogen, and mixtures of nitrogen and hydrogen; (2) holding said heated catalyst in said atmosphere at said temperature of greater than 1200.degree. F. for at least 10 minutes; (3) contacting said catalyst at said temperature of greater than 1200.degree. F. with a dry activating gas comprising a halosilane selected from the group consisting of chlorosilanes and bromosilanes for a time sufficient to incorporate a halide content to the catalyst and to increase the activity of the catalyst, said contacting step (3) being carried out in the absence of air; (4) cooling said halosilane contacted catalyst of step (3), and

b. recovering an isomerized hydrocarbon from step (a).

2. A process according to claim 1 wherein said hydrocarbon is n-butane.

3. A process according to claim 1 wherein said isomerization conditions are a temperature of 100.degree. to 600.degree. F. under pressure of atmospheric to 1500 psig and wherein said process is carried out at a liquid hourly space velocity of 0.1 to 15 volumes of liquid charged per volume of catalyst.

4. A process according to claim 3 wherein said hydrocarbon is n-butane.

5. A hydrocarbon skeletal isomerization process which comprises:

a. contacting an isomerizable hydrocarbon selected from the group consisting of acyclic paraffin and naphthene under isomerization conditions with an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst activated by (1) passing a dry activating gas comprising a halosilane through a bed of alumina at a temperature of greater than 1200.degree. F.; (2) passing the effluent from said alumina bed of step (1) directly into contact with said alumina-supported metal catalyst which is also at a temperature of greater than 1200.degree. F. for a time sufficient to incorporate a halide content to the catalyst and to increase the activity of the catalyst; (3) cooling said halosilane-contacted catalyst of step (2), and;

b. recovering an isomerized hydrocarbon from step (a).

6. A process according to claim 5 wherein said hydrocarbon is n-butane.

7. A process according to claim 5 wherein said isomerization conditions are a temperature of 100.degree. to 600.degree. F. under pressure of atmospheric to 1500 psig and wherein said process is carried out at a liquid hourly space velocity of 0.1 to 15 volumes of liquid charged per volume of catalyst.

8. A process according to claim 7 wherein said hydrocarbon is n-butane.

9. A hydrocarbon skeletal isomerization process which comprises:

a. contacting an isomerizable hydrocarbon selected from the group consisting of acyclic paraffin and naphthene under isomerizaton conditions with an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst activated by (1) heating said catalyst to a temperature of greater than 1200.degree. F. in an atmosphere of nitrogen and hydrogen; (2) holding said heated catalyst at said temperature in a hydrogen atmosphere in the substantial absence of nitrogen for a time of at least 10 minutes; (3) contacting said heated catalyst of step (2) with a dry activating gas comprising a chlorosilane to incorporate chlorine as chloride ion to said catalyst; (4) cooling said catalyst of step (3) to a temperature of 1100.degree. F. in the presence of hydrogen and the absence of nitrogen; (5) cooling said catalyst of step (4) in the presence of nitrogen and hydrogen, and

b. recovering an isomerized product from step (a).

10. A process according to claim 9 wherein said hydrocarbon is n-butane.

11. A process according to claim 9 wherein said isomerization conditions are a temperature of 100.degree. to 600.degree. F. under pressure of atmospheric to 1500 psig and wherein said process is carried out at a liquid hourly space velocity of 0.1 to 15 volumes of liquid charged per volume of catalyst.

12. A process according to claim 11 wherein said hydrocarbon is n-butane.

13. A hydrocarbon hydrocracking process which comprises:

a. contacting a hydrocarbon under hydrocracking conditions with an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst activated by (1) heating said catalyst to a temperature of greater than 1200.degree. F. in an atmosphere selected from the group consisting of nitrogen, hydrogen, and mixtures of nitrogen and hydrogen; (2) holding said heated catalyst in said atmosphere at said temperature of greater than 1200.degree. F. for at least 10 minutes; (3) contacting said heated catalyst of step (2) at said temperature of greater than 1200.degree. F. with a dry activating gas comprising a halosilane selected from the group consisting of chlorosilanes and bromosilanes for a time sufficient to incorporate a halide content to the catalyst and to increase the activity of the catalyst, said contacting step (3) being carried out in the absence of air; (4) cooling said halosilane-contacted catalyst of step (3), and

b. recovering a hydrocracked product from step (a).

14. A hydrocarbon hydrocracking process which comprises:

a. contacting a hydrocarbon under hydrocracking conditions with an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst activated by (1) passing a dry activating gas comprising a halosilane through a bed of alumina at a temperature of greater than 1200.degree. F.; (2) passing the effluent from said alumina bed of step (1) directly into contact with said alumina supported metal catalyst which is also at a temperature of greater than 1200.degree. F. for a time sufficient to incorporate a halide content to the catalyst and to increase the activity of the catalyst; (3) cooling said halosilane contacted catalyst of step (2), and

b. recovering a hydrocracked product from step (a).

15. A hydrocarbon hydrocracking process which comprises:

a. contacting a hydrocarbon under hydrocracking conditions with an active alumina-supported Pt, Ir, Os, Ru, Rh, or Pd metal catalyst activated by (1) heating said catalyst to a temperature of greater than 1200.degree. F. in an atmosphere of nitrogen and hydrogen; (2) holding said heated catalyst in said atmosphere at said temperature in a hydrogen atmosphere in the substantial absence of nitrogen for a time of at least 10 minutes; (3) contacting said heated catalyst of step (2) with a dry activating gas comprising a chlorosilane to incorporate chlorine as chloride ion to said catalyst; (4) cooling said catalyst of step (3) to a temperature of 1100.degree. F. in the presence of hydrogen and the absence of nitrogen; (5) cooling said catalyst of step (4) in the presence of nitrogen and hydrogen, and

b. recovering a hydrocracked product from step (a).

16. The process of according to claim 1 wherein HCl is used in conjunction with said halosilane.