DE2117651A1 - Catalyst for the conversion of hydrocarbons, its manufacture and use - Google Patents

Description

Cologne, April 5th, 1971 Fu / Ax

Britannic House, Moor Lane, London, E.C. 2 (England).

Catalyst for the Umwandlu ng v on hydrocarbons,

ίί? - ¹ !! ^ osition and use.

The invention "relates to platinum-containing catalysts and their use for the catalytic conversion of hydrocarbons «

Catalysts containing platinum on a refractory support are well known. The platinum, which may be in an amount of 0.1 to 5 % by weight, has good activity for hydrogenation or dehydrogenation and dehydrocyclization depending on the process conditions. Through a suitable choice of the support, additional functions, for example isomerization and cracking, can be imparted to the catalyst.

Since platinum is an expensive metal, there are methods of degradation the platinum content of such catalysts is very important without affecting their properties and performance and beneficial. Recently, the development of bimetal catalysts has attracted a lot of interest. It has now been found that both the type of second metal and the proportion of this metal in the ratio are important to platinum «In particular, it has been found that graphs of the activity of the catalyst clear peaks depending on the amount of metal show corresponding to certain compositions.

1098U / 1622

The invention 0.01 to 10 Ge \] _o -% metal containing on a refractory support, suitable for the conversion of hydrocarbons catalysts, which are characterized in that they contain platinum and a constituent with platinum solid solution second metal, the atomic amounts of the platinum and the second metal being substantially equivalent to the amounts which form ordered alloy structures.

The metallurgy of platinum alloys is well established _o metals known to be solid with platinum

™ Form solutions are, for example, cobalt, liiekel, iron, Copper, tin, palladium, iridium, rhodium, silver, gold, bismuth, mercury, antimony, lead and cadmium, according to These firmly established metallurgical principles can be traced back to the existence of ordered structures in all Easily identify bimetal systems. Many of them are already known. These ordered structures contain the two metals in a simple atomic ratio. The ratios can be different for different metals, but for any two metals there is relative poorly ordered structures, usually five at most. The most common are

) AB, i.e. 50 atom- $ A and 50 atom-jä B

Α-, Β, i.e. 75 atom- ^ A and 25 atom- ^ B A ₇ B, i.e. 87.5 atom-ji A and 12.5 atom-fi B-

Other ratios that can occur with certain systems are A- ^ Bp and A, B, but they can, as already mentioned, can be detected in every system according to the usual methods,

With the above-mentioned second metals, it is known that the following proportions of platinum and the second result Metal-ordered structures:

108844 / 1S22

3 PtCo PtSn ₂ PtCo ₅ PtSn ₄ PtNi PtIi ₅ Pt ₅ Fe PtFe PtFe ₅ Pt _? Cu Pt ₅ Cu PtCu PtCu ₅ Pt ₇ Sn Pt ₅ Sn PtSn Pt ₂ Sn ₅ PtBi ₂ Pt ₇ Pd PtPd PtHg ₂ PtHg ₄ ι Pt ₅ Ag PtAg. PtSb ₂ PtAg ₅ PtAu ₅ PtPb ₄ PtBi PtCd ₂ PtBi ₅ Pt ₂ Cd ₉ PtHg Pt ₄ Sb Pt ₅ Sb 2 PtSb Pt ₅ Pb PtPb Pt ₅ Cd

The ordered structures Pt ^ Sn and PtCo ₅ have not yet been reported, but their existence can be assumed from the results described below. Evidence for the presence of ordered platinum-palladium structures around Pt ~ Pd and PtPd has been published, but their exact composition is less clear. The possibility of ordered structures in platinum-iridium and platinum-rhodium alloys exists, but the published evidence is inconclusive.

The term ⁿ substantially equivalent to the quantities that make up ordered structures "means +5 atom- $ for each metal.

The platinum is preferably present in the same amount or in a greater amount than the other metal »Preferably is the platinum content at least 45 atomic? ». The preferred second metals are cobalt, Nickel, iron, copper, tin and palladium.

The invention also includes the manufacture of catalysts useful for the conversion of hydrocarbons

10984 4/1622

BATH ORIGINAL

are suitable and contain 0.01 to 10 G-ew _e - ^ metal on a refractory carrier, according to a method which is characterized in that the carrier with a solution containing platinum ions and a solution containing ions of a zv A metal which forms a solid solution with platinum is treated, the concentration of the ions in the solutions and the conditions of the treatment being chosen so that the amounts of the platinum and the second metal on the catalyst are the same as the ordered amounts Form alloy structures are essentially equivalent.

The carrier can be treated with the same solutions containing ions of the platinum and the second metal, simultaneously or sequentially in any order. The treatment is preferably carried out one after the other, the platinum-containing solution being used first.

The platinum and the second metal can be deposited by ion exchange. This familiar expression means that the ions chemically combine with active sites on the surface of the support. Especially with carriers who contain few or weak active sites, the wearer should be washed exhaustively with water while the fc ions are still in the water-soluble state until the wash water is free of metal ions. Through this laundry · ensures that the only metal that is on the The carrier remains, is in ion-exchanged form. The platinum ions and the ions of the second metal can can be added both in the form of cations and anions. The cations are preferred, as most are common ones Carriers are cation exchangers. The platinum and the second metal can also be impregnated in can be applied in the usual way. This way of working is particularly preferred «

. The term "metal ions" includes complex ions, where the metal are to a ligand, in particular water, ammonium, or halogen, Se] J ¹ JMfA 4 ⁸ ^ ji ^ tf3> ^CLLE complex ions

_ 5 -

usual form of ions "with many metals in aqueous or ammoniacal solution. The normal ones containing platinum Solutions that are used for the production of catalysts therefore consist of Ietramminplatin (II) chloride, which gives tetrammine platinum (II) cations, and chloroplatinic acid, the hexachloroplatinate anions gives »The second metal solution can be any suitable salt, e.g. the chloride, nitrate or acetate, and in turn be an ammoniacal solution.

The conditions of treatment with the ions of the platinum and the second metal, ie the temperature, the time and the concentration of the ions in the solution, depend on the ease of uptake and the desired uptake and, if necessary, can easily be determined experimentally . Be suitable temperatures proven treatment times of 10 to 11O ⁰ C, of 1 to 72 hours, and solution concentrations of 0.001 to 2 molar.

In the manufacture of ion-exchanged catalysts, deionized water is expediently used for washing to remove unbound ions. As already mentioned, washing is carried out until the washing water is free of ions of the platinum and the second metal. The temperature can likewise be from 10 to 110 ^° C. and the treatment time from 1 to 72 hours. Preferably, 2 to 100 ml of water / ml of catalyst are used.

As refractory inorganic oxides T _r äger preferably of elements of Groups II, III and IV of the periodic table, mixtures of two or more such oxides or compounds containing one or more such oxides in their Bruttoforrael be used. Silicon dioxide and aluminum oxide are preferred as binoxides. The preferred mixed oxides are silicon dioxide-aluminum oxide, silicon dioxide-magnesium oxide and boron oxide-aluminum oxide, and the aluminosilicates, for example zeolites, are preferred as minerals.

The catalysts can also 0.1 to 8 wt φ a halogen, in particular chlorine, contain "

After the addition of the metals can dry the catalyst, for example 1 to 24 hours at 50 to 110 ⁰ C, and calcined for 1 to 24 hours at 250 to 6CO C. Suitably, the catalysts prior to use can be reduced by being heated for 1 to 24 hours at 200 to 60G ⁰ C in a reducing atmosphere. Flowing hydrogen is preferably used as the reducing atmosphere. The reduction of the bimetal catalyst can be more difficult than the reduction of catalysts that only contain platinum. Care must be taken to ensure the reduction Hand of the hydrogen uptake from a closed system in which hydrogen is circulated over the catalyst can be monitored «

The invention encompasses the catalytic conversion of hydrocarbons by a process in which the hydrocarbons are converted under conversion conditions with a catalyst brings together the platinum and a second metal on a refractory support in the above composition contains.

The conversion conditions can vary widely, depending on the feedstock and the reaction, however, work is usually done within the following areas

Temperature 0-600 ° G

Pressure 0-210 atm

Room flow rate 0.1-20 V / V / hour.

Hydrogen / hydrocarbon molar ratio

ratio Os1 to 20s1

The preferred hydrocarbons as starting materials can be derived from any suitable source, e.g. from petroleum, and its exact nature depends on the required reaction from

108844 / 1S22

Paraffins and / or olefins and / or naphthenes, in particular, are used for the dehydrogenation and dehydrocyclization those with 3 to 25 carbon atoms are preferred as hydrocarbons. The preferred dehydrogenation or dehydrocyclization reactions can be performed under the following conditions:

Temperature - 300 - 600 ⁰ C

Pressure 70 atm

Rough flow rate 0.1 - 10 V / V / hour.

Hydrogen / hydrocarbon molar ratio 0; 1 to 20: 1

For example, the catalysts according to the invention can be used for the catalytic reforming of hydrocarbons boiling in the gasoline range (15 to 204 ° C.), in particular petroleum fractions, in order to increase the aromatic content and / or the oetane number. Preferred carriers for this purpose is alumina, which may be 0.1 to 8 wt - $ contains halogen.. Such a carrier has the modest isomerization and cracking activity usually believed to be desirable in catalytic reforming.

Unsaturated starting materials are used for hydrogenation reactions Hydrocarbons, e.g. acetylenes, olefins or aromatics, especially those with 2 to 20 carbon atoms, in Question. These reactions can be carried out under the following conditions:

Temperature 0-300 ⁰ C

Pressure * HO atü

Room flow rate 0.1-20 V / V / hour.

Hydrogen / hydrocarbon molar ratio 0.001: 1 to 20: 1

The catalyst support is preferably relatively inert for hydrogenation reactions. For example, are suitable Silica, sepiolite, and alumina of low acidity.

109844/1622

example 1

A series of platinum-copper catalysts was produced. Silicon dioxide with a particle size of 0.25 "to 0.5 mm and a surface area of 170 m / g (manufacturer Hopkins and Williams Ltd") was used as the carrier. The carrier was through washing "liberated with normal HCl and distilled water of iron impurities a catalyst containing 1.8 Gewo-fo platinum, was prepared as follows: 100 g of fumed silica were mixed with 9, 22 ml of a molar solution of tetrammineplatinum (II) chloride 2 hours Treated at 25 ° C. The silica was then washed with 50 ml aliquots of deionized water at 25 ° C. The wash water that ran off at the end was free of plationions. The catalyst was dried for 24 hours at 110 ⁰ O.

A number of platinum-copper catalysts were prepared as follows: The concentration of the tetrammine platinum (H) chloride in the solution was gradually decreased and the Pt-

SiO ₂ treated with solutions of copper (II) chloride in aqueous ammonia with a specific gravity of 0.880 with a gradually increasing concentration. The relative concentrations were adjusted so that each catalyst the same metal content in g-atom had such as 1.8 wt. -ΗΌ platinum on silica-containing catalyst, however, the Pt and Cu in various atomic ratios of 90:10, 80:20, 70:30 and so on. In the last catalyst, the treatment with platinum was completely omitted, a catalyst with 0.59% by weight copper on silicon dioxide being obtained. Washing and drying after each treatment with the copper solution were carried out in the same manner as in the treatment with the platinum solution.

Each catalyst was dried for 24 hours at 110 ^° C. and for 3 hours at 500 ^° C. in hydrogen, which was present in an amount of 4000 V / V / hour. was used, reduced. The examination by electron spin resonance and the measurement of the hydrogen uptake during the reduction confirmed that the

1098U / 1622

Metal had been reduced. Each catalyst was used for the dehydrogenation and dei ^ drocyclization of η-hexane "at 500 ° C and normal pressure used «The starting material consisting of hydrogen and n-hexane (molar ratio EL / n-hexane = 10: 1) was used in an amount of 4000 V / V / h. fed.

The results are shown in Table 1 below and as

—1 —1 2 conversion expressed in mmol min. G 10.

Table 1 Conversion to benzene, Atomic amount of platinum Total sales mmol min. ~ ¹ g ~ ¹ x10 ² in the catalyst, ^ mmol Min. ~ ¹ g " ¹ x 10 ² 3.4 100 13.3 5.1 90 18.0 3.7 80 14.2 3.7 70 12.8 2.3. 60 7.8 2.7 50 13.3 1.2 40 12.8 1.2 30th 5.6 0.3 20th 9.4 0.1 10 3.6 0 0 0

The conversion products obtained other than benzene consisted mainly of hexene and coke.

Example 2

Aluminum oxide, which is obtained by calcining an aluminum oxide hydrate precursor, in which the trihydrates predominated, had been produced, a surface area of 242 m / g, a pore volume of 0.37 ml / g and a particle size of 0.19 to 0.25 mm was used with chloroplatinic acid in such an amount impregnated that a catalyst containing 0.6 wt .- ^ platinum was obtained. A number of platinum-copper catalysts were also used in that described in Example 1 Way by gradually reducing the

109844/1622

put the amount of platinum and impregnation with the Pt-AlpO ^ Copper (ll) chloride solution in amounts that are gradually increasing Copper contents showed, produced «the i-: en-ratios were adjusted so that each catalyst had the same total metal content in g-Atoia as the 0.6 wt. Catalyst containing platinum on alumina, but had different atomic ratios of Pt and Cu from 90:10, 80:20, 70:30, etc. A $ 100 catalyst Cu was also produced.

Each catalyst was dried overnight at 110 ⁰ C, for 3 hours at 50O ⁰ C in 4000 V / V / hr. V / on Hydrogen reduces · and tested to determine its activity for the dehydrocyclization using η-hexane as the starting material referred to in Example 1, process conditions (500 ⁰ C, normal pressure, 4000 V / V / hr. Feedstock having an H ₂ / n- Hexane molar ratio of 10: 1).

The results obtained are given below in Table 2 and are expressed as conversions in mmol min. "G" ~.

1098U / 1622

Atomic amount
Pt, 51 total
sales Sales too
benzene Selecti
vity for
Benzoil, # Tabel 2 sales
Xylenes to Selek
tivi
for
Xylenes 4.8 total
sales
to Aro-
rr.at 2 η Selectivi
for
Overall ao
ma ten, # 100 0.25 0.11 44.2 Sales too
toluene Selek
tivi
for
toluene - _ 10 0.13 51.5 90 0.33 0.16 49.5 0.02 7.3 0.02 12.3 0.21 61.8 80 0.25 0.13 51.6 0.03 7.5 0.03 6.8 0.18 70.5 70 0.27 0.20 73.4 0.02 8.9 0.03 12.9 0.26 95 60 0.16 0.11 65.0. 0.03 9.3 0.01 9.5 0.13 78.2 ο 50 0.30 0.15 51 0.01 6.4 0.04 11.8 0.21 72.5 co • 4 ° 0.21 0.07 33 0.02 8.5 0.02 11.8 0.11 52 » OO
* ■ - 30th 0.17 0.06 41 0.01 9.5 0.02 25th 0.10 52.7 - ■ C- 20th 0.17 0.06 35 0.01 5.9 0.03 _ __ 0.09 52.7 ' co 10 0.12 0.05 42 0.01 5.9 0.03 0.09 75.3 ro 0 0.04 track _ 0.01 8.3 Sour 0.22 58 ro track _

Example 3

Aluminum oxide obtained by calcining an aluminum oxide hydrate precursor, in which the trihydrates predominated,

and had a surface area of 242 m / g, a pore volume of 0.37 ml / g and a particle size of 0.19 to 0.25 mm, was impregnated with chloroplatinic acid in such an amount that a catalyst containing 0 , 6 wt .- / o platinum was obtained. A number of platinum-cobalt catalysts have also been produced by gradually reducing the concentration of the chloroplatinic acid in the solution and impregnating the Pt-AlgO with cobalt- W chloride solutions with gradually increasing concentrations. The proportions were adjusted so that each catalyst the same total metal content in g-Atomenwie of 0.6 wt _o - $> platinum on alumina catalyst containing ,, but different atomic ratios of Pt and Co of 90:10, 80:20, 70: 30 etc. had. A $ 100 Co catalyst was also made.

Each catalyst was ^{dried overnight at 110 °} C., 3 hours at 500 ^° C. in 4000 V / V / hour. Hydrogen and reduced to activity for dehydrocyclization using η-hexane as starting material at 500 ° C, normal pressure and 4000 V / V / hr ₀ starting material with an "H ₂ / n-hexane Mo! Ratio of 10: 1 checked.

j The results are given in Table 3 below and

- 1 - 1 expressed as conversions in mmol min. G.

109844/1622

Speed of formation
in mmol min. "* ¹ g ~ ¹ toluene - Xylenes S e Tabel 3 ä t Total sales,
mmol Min. "" ¹ g ~ ¹ Atomic amount
Platinum, $ benzene 0.015 0.018 benzene 1 e k t i ν i t Total aromatics 0.13 0.014 0.019 46.5 toluene Xylenes 58.0 0.28 100 0.15 0.017 0.024 58 5.2 6.3 70.9 0.26 90 0.18 0.015 0.026 - 64.5 5.5 7.4 79.4 0.28 80 0.15 0.014 0.020 58 6.2 8.7 73.8 0.26 70 0.14 0.016 0.027 61 5.8 10 75.5 0.23 60 0.17 0.013 0.017 68 5.9 8.6 85.1 0.25 50 0.09 0.008 0.028 39 6.3 10.8 43.1 0.23 40 0.05 0.013 0.038 27.8 5.6 7.5 47i3 . 0.18 30th 0.06 - 0.009 35 4.5 15th 65.2 0.17 20th 0.003 - 10 7.8 22.4 40 • 0.03 10 - - - 30th - 0.004 . 0 - -

-H-

The results obtained in the experiments described in Examples 1, 2 and 3 for the formation of benzene from the used η-hexane (ie the activity for the dehydrocyclization) are shown graphically in FIG. The graph clearly shows the large fluctuations in the activities depending on the Pt-Cu and Pt-Co atomic ratios and the pronounced peaks that correspond to ordered structures. These ordered structures with high platinum content had significantly higher activities than the 100 atom $ Cu catalyst.

The peak in Pt ^ Cu can be compared to the absence of any peak in Pt-Co. In the Pt-Co system, there is no corresponding ordered structure. No measurements were made for 75 ^ Pt and 255 ^ Cu or 75 ^ Pt and 25 $ 6 Co (Pt ₅ Cu or Pt ^ Co), so that the tips are slightly shifted. Although the Pt-Cu-SiOp catalysts had a low activity, the presence of peaks can still be seen. The catalysts containing platinum in amounts of 40 atoms $ or less had relatively low activities, but the curves still show a non-linear effect in this area including a distinct peak in the Pt-Co curve T

Example 4

A range of platinum-nickel-alumina catalysts and platinum-iron-alumina catalysts were prepared in the manner described in Example 3, however using nickel chloride (NiCIp) or iron chloride (FeCl,) instead of cobalt chloride. The catalysts were tested for activity for dehydrocyclization, again with the same feedstock was carried out under the same process conditions as in Example 3. The results are below mentioned in Tables 4 and 5.

109844/1622

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C • Η 4 = ¹ CO

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in 36.2 53.5 in
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10984W1622

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W. τ- O O O O O O ο Ο 3 " ο in in ιΗ
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■ Η O Ό τ— (M _T _ α I Ql O ro in O CM CM v— co • Η r-l C CM CM CM CM CM τ— I. Ι5 O CS in «Ι O O O * £ 2 N Ό CM O O O O O O O CJ r-l O O O O CO
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-P N O ZS Q -P τ— ¹ Xl CO CO γ-Η CO E) ■ Η φ Θ pq CU 3

109844/1622

The results for benzene formation obtained in the experiment described in Example 4 are graphed in FIG. 2 Also shown in Figo2 are the results with a Series of platinum-alumina catalysts shown with decreasing platinum content. As in Fig. 1 are Tips, which correspond to ordered structures, are clearly visible. These tips leave one in most cases Detect activity higher than the activity of a 100 atom platinum catalyst. The straight one Curve for the Pt-AlpO ^ catalysts with decreasing Platinum content provides a baseline for comparison and shows that the peaks are not due to a platinum thinning effect are due.

Example 5

A series of platinum-palladium-alumina catalysts and a series of platinum-tin-alumina catalysts (over the range of 100 to 50 atomic $ Pt) were prepared in the manner described in Example 3 but using PdCl ₂ and SnCIp produced instead of cobalt chloride. The catalysts were examined for their activity for the dehydrocyclization, again using the starting material mentioned in Example 3 and the process conditions mentioned there. The results for the Pt-Pd-AlgO ^ catalysts are shown in Table 6 below.

109844/1622

Table 6

ο co OO

cn

BO

io platinum Pla1
Speed of formation
mmole mine " ¹ g ~ ¹ benzene Xylenes tin-PalMi um aluminum oxide
S e 1 ect Xylenes i ν i t ä t Total aromatics 90 Total-.
sales 0.16 0.006 toluene benzene 2.3 toluene 66.5 80 0.26 0.14 0.004 0.007 61.5 1.5 2.7 55.5 70 0.27 0.11 0.001 0.004 52.5 0.3 1.5 42.3 60 0.27 0.088 track 0.003 41 - 1.0 40.3 50 ■ 0.22 0.12 dd 0.001 40 - s 0.3 48 40 0.26 0.11 Il 0.004 46.5 - 1.5 44 30th 0.26 0.092 0.009 0.004 42.5 4.5 ¹ » ⁵ 5.2.5 20th 0.20 0.080 track 0.004 46 - 2.0 43.6 10 0.19 0.038 0.011 0.003 42 1.3. 1.6 43.3 0 0.08 0.014 track track 42 _ - 20th 0.07 track 20th -

CO I

O)

cn

With the platinum-tin-alumina catalysts, the following results were obtained on the rate of formation obtained from benzene:

^u / a Pt benzene formation rate

mmol Min. " ¹ £ ~ ¹

100 0.13

90 ■ 0.296

80 0.219

70 0.267

60-0.175

50 '0.204

With these catalysts, too, fluctuations can be seen over the entire range. The platinum-falladium-aluminum oxide catalysts of Table 6 show maxiaa at 90 Pt: 10 Pd (corresponding to the probable ordered structure Pt ₇ Pd) and 50 Pt: 50 Pd (corresponding to the probable ordered structure PtPd) ₀

The results with the platinum-tin-aluminum oxide catalysts are particularly interesting not only in the maxima at 90:10 (Pt ₇ Sn) -, 70:30 (Pt ₃ SnX) and 50:50 (PtSn), but also with regard to the Significant increase in activity due to the tin compared to the catalyst containing 100 $ Pt.

A comparison of the best result with each metal in Examples 2 through 5 with 100 atom- ^ Pt gives the following relative improvements through the addition of a second metal in a proportion that is an ordered structure equivalent is:

100 atom -? $ Pt 100

TOfo Pt 30 $ Cu (Pt ₅ Gu) 155

80 / ί Pt 20 <£ Oo (Pt ₅ Go) HO

$ Pt 5O ^ Hi (PtWi) 155

yS Pt 2Ο5 & Fe (Pt ₅ Fe) 145

109844/1622

90 $ Pt 1096 Pd (Pt ₇ Pd) 125

90 $ Pt 10 $ Sn (Pt ₇ Sn) 225 '■

Example 6

Samples of the platinum-copper-aluminum oxide catalysts prepared according to Example 2 with the atomic ratios 70:30, 60:40 and 50:50 were longer time with increased Pressure used under the following conditions:

! Temperature 500 C

Pressure 24.5 atm

Feedstock 'n-heptane

Room flow velocity 6.0 V / V / hour «

Hydrogen / hydrocarbon molar ratio . 7: 1

Duration 48 hours

The products were analyzed by gas-liquid chromatography. The following conversion of the n-heptane into aromatics was achieved:

Conversion to aromatics, Mon 1- $ At the beginning At the end

70 $ Pt 305ε Cu, 50 40

60 $ Pt 40/0 Cu 30 20

$ 50 pt 50? $ Cu 45 35

These results confirm the previous findings that metal content catalysts are the ordered. Structures correspond to (70 $ Pt 30 $ Cu ^ s Pt, Cu and 50 $ Pt 50 $ Cu = PtCu) are significantly more active than a catalyst with 60 $ Pt and 40 $ Cu, i.e. a quantity ratio that does not correspond to any ordered structure »The results confirm that this finding applies to increased pressure, and that the increased activity is maintained for long periods of time "

109844/1622

Claims (1)

Claims In that the catalyst comprises platinum and a forming platinum solid solution second metal contains% deposited metal consists, characterized in that the atomic quantities - 1. A catalyst for the conversion of hydrocarbons which consists of a refractory support material and from 0.01 to 10 wt. of the platinum and second metal are substantially equivalent to the amounts that form ordered alloy structures. 2. Catalyst according to claim 1, characterized in that that the second metal is cobalt, nickel, iron, copper, tin, palladium, iridium, rhodium, silver, gold, bismuth, Mercury, antimony, lead or cadmium. 5. Catalyst according to Claims 1 and 2, characterized in that that it contains at least 45 atomic # platinum. 4. Catalyst according to claims 1 to ~ 5, characterized in that the metals in the ordered alloy structures of Pt ₃ Co, PtCo, PtNi, Pt ₃ Fe, PtFe, Pt ₇ Cu, Pt, Cu, PtCu, Pt ₇ Sn, Pt ₃ Sn, PtSn, Pt ₇ Pd or PtPd are present. 5. Catalyst according to claims 1 to 4, characterized in that the carrier material is aluminum oxide, the optionally contains 0.1 to 8 wt .- ^ halogen. - 22 - 109844/1622 6. A process for manufacturing a catalyst for · conversion of hydrocarbons which consists of a refractory support material and from 0.01 to 10 wt -% deposited metal, characterized in that 'the carrier material is treated with a platinum ion-containing solution and a solution. containing ions of a second metal which form a solid solution with platinum, the concentrations of the ions in the solutions and the reaction conditions being selected such that the atomic amounts of the platinum and the second metal are substantially equivalent to the amounts that form the ordered alloy structures form. 7. The method according to claim 6, characterized in that that the carrier material with the platinum ions and the ions of the second metal simultaneously or in any Order is handled. 8. Use of the catalyst according to Claims 1 to 5 Conversion of hydrocarbons, characterized in that the hydrocarbons are at a temperature of 0 to 600 ° C, a pressure of 0 to 210 atü, at a Space flow rate of 0.1 to 20 V / V / h and a hydrogen / hydrocarbon molar ratio of 0 to 20: 1 are passed over a catalyst that contains platinum and a second metal, the platinum forms a solid solution, the atomic amounts of the platinum and the second metal being essentially the same are equivalent, which lead to ordered alloy structures. - 23 - 109844/1622 9. Use according to claim 8, characterized in that that carbon fiber with 3 to 25 carbon atoms at a temperature of 300 to 600 ° C, - a pressure from 0 to 70 atmospheres, a «space flow velocity dehydrogenated from 0.1 to 10 V / V / h and a hydrogen / hydrocarbon molar ratio of 0 to 20: 1 or be dehydrocyclized. lo. Use according to claims 8 and 9, characterized in that that the catalyst for the catalytic reforming of gasoline fractions ranging from 15 to Boil 20 '+ ° C, is used. 10984 / f / 1622