Catalytic hydroreforming process

Abstract

Process for reforming hydrocarbons or producing aromatic hydrocarbons under severe operating conditions, in the presence of a catalyst comprising an alumina carrier and, expressed by weight with respect to alumina:(a) from 0.05 to 0.6% of platinum(b) from 0.01 to 2% of rhenium(c) from 0.05 to 3% of thallium or indium, and(d) from 0.1 to 10% of a halogen.

Description

This invention relates to new catalysts and a catalytic reforming process as well as a catalytic process for manufacturing aromatic hydrocarbons, said processes being conducted under severe conditions and in the presence of one of these new catalysts. These processes are conducted at a temperature from 510.degree. to 600.degree. C. under a pressure from 1 to 13 kg/cm.sup.2 at a hourly space velocity from 1 to 10 volumes of liquid charge per volume of catalyst, the ratio hydrogen/hydrocarbons being from 5 to 20.

More precisely, these new catalysts can be used for:

Reforming reactions, in order to obtain a gasoline with a clear octane number of at least 102. The severe conditions of the catalytic hydroreforming reactions are more particularly as follows: average temperature from about 510.degree. to 580.degree. C., pressure from about 5 to 18 kg/cm.sup.2, preferably 6 to 13 kg/cm.sup.2, hourly space velocity from 1 to 10 volumes of liquid naphtha per volume of catalyst and recycle rate from 6 to 10 moles of hydrogen per mole of charge. The charge is generally a naphtha distilling between about 60.degree. C. and about 220.degree. C., particularly a straight run naphtha.

Reactions for producing aromatic hydrocarbons from saturated or unsaturated gasolines (for the production of benzene, toluene and xylenes). In the case of an unsaturated charge, i.e. which contains diolefins and monoolefins, the charge must be first made free thereof by selective or total hydrogenation. Subsequently, the charge, free of substantially all diolefins and monoolefins previously contained therein, is subjected to a treatment with hydrogen in the presence of a catalyst at a temperature from about 530.degree. to 600.degree. C., under a pressure from 1 to 13 kg/cm.sup.2, the hourly feed rate by volume of the liquid charge being of about 1 to 10 times the volume of the catalyst, the molar ratio hydrogen/hydrocarbons being from about 6 to 20. The charge may consist of pyrolysis gasoline, cracking gasoline, particularly steam-cracking gasoline, or catalytic reforming gasoline or still may consist of naphthenic hydrocarbons convertible to aromatic hydrocarbons by dehydrogenation.

Catalysts containing platinum deposited on alumina have been known for a long time. But, in spite of a number of improvements made to these catalysts, for example by incorporating thereto one, two or even three additives such as rhenium, germanium, tungsten, molybdenum or several other metals of any group of the periodic classification of elements, it is still desired to-day to find new catalysts which, on the one hand, would give still better yields than those obtained up to now and which, on the other hand, would have a longer life time than that of the known catalysts. In addition, an attempt is made to improve the mechanical properties of these catalysts in order to allow their use in a moving bed in the form of conglomerates, for example balls or extrudates of a substantial size, so as to leave a relatively free passageway to gaseous reactants. The wear of these catalysts results in the formation of much thinner grains which clog progressively the free space and oblige to increase the inlet pressure of the reactants or even to discontinue the operation. While it was known that in reforming reactions high yields were obtained particularly by use of a catalyst with a porous carrier base (particularly alumina) containing, for example, simultaneously platinum and/or another noble metal of the platinum family, and another metal such, for example, as copper, gold, silver and iridium, it has been now discovered that when proceeding in the presence of other specific catalysts, specially in a moving bed, the latter catalysts exhibited, in the reactions of hydroreforming and aromatic hydrocarbon production, an increased activity and, above all, an increased life-time as compared to the prior art catalysts.

The specific catalyst used in this invention comprises an alumina carrier, platinum, rhenium, thallium or indium and a halogen, for example chlorine or fluorine.

The catalyst of the invention contains, expressed by weight with respect to the alumina carrier: (a) from 0.05 to 0.6% and more particularly 0.1 to 0.3% of platinum, (b) 0.01 to 2% and preferably 0.1 to 0.25% of rhenium, (c) from 0.05 to 3%, preferably 0.07 to 2% and, more particularly, 0.3 to 0.6% of thallium or indium and (d) from 0.1 to 10% and preferably 0.2 to 5%, by weight with respect to the alumina carrier, of a halogen, for example chlorine or fluorine.

The textural characteristics of the alumina may also be of importance: in order to proceed with sufficiently high space velocities while avoiding the use of reactors of excessivley large capacity and of an excessive amount of catalyst, the specific surface of the alumina may be advantageously from 50 to 600 m.sup.2 per gram, preferably from 150 to 400 m.sup.2 /g.

The catalyst may be prepared according to conventional methods consisting of impregnating the alumina with solutions of compounds of the metals to be introduced; either with a common solution of these metal compounds or with a separate solution for each metal compound.

When using several solutions, intermediate drying and/or calcination steps may be performed. The operation is completed by a calcination, e.g at about 500.degree. to 1000.degree. C., preferably in the presence of free oxygen, for example by air scavenging.

Examples of metal compounds introduced in the composition of the catalyst are the nitrates, chlorides, bromides, fluorides, sulfates, ammonium salts or acetates of these metals or even any other salt or oxide of these metals soluble in water, in hydrochloric acid or in any other suitable solvent.

The halogen of the catalyst may be supplied from one of the metal halides when the metal is introduced as a halide, or may be introduced in the form of hydrochloric acid, hydrofluoric acid, ammonium chloride, ammonium fluoride, gaseous chlorine or hydrocarbon halide, e.g CCl.sub.4, CH.sub.2 Cl.sub.2 or CH.sub.3 Cl.

A first method of preparation consists, for example, of impregnating the carrier with an aqueous solution of indium or thallium nitrate or other compound, drying at about 120.degree. C. and calcining in air for a few hours at a temperature from 500.degree. to 1000.degree. C., preferably about 700.degree. C.; a second impregnation will then be performed with a solution containing rhenium and platinum.

Another method consists, for example, of impregnating the carrier with a solution containing simultaneously the three metals of the catalyst.

Still another method consists of introducing the metal elements by a number of successive impregnations equal to the number of metal elements to be introduced into the catalyst.

The production of a gasoline of very high octane number necessitates the use of very severe conditions which are not easily withstood by the catalysts used up to now. The use of bimetallic catalysts however, resulted in a significant improvement. Numerous attempts to associate various metals have been made and, recently, catalyst compositions containing up to 4 metals have been proposed. These compositions, in fact, resulted in an improvement but, generally, the promoters, when favorable to the stability properties, unhappily exhibit, particularly as concerns noble metals of the platinum family, a certain tendency to hydrogenolysis, which definitively results in decreased yields, in a shortening of the cycle period and in a decrease in the possible number of cycles, i.e. in a decrease of the life-time in the catalyst.

On the contrary, the simultaneous use of rhenium and thallium or indium in combination with platinum, very significantly reduces this hydrogenolyzing tendency, and it has been observed that the benefits resulting from the simultaneous use of rhenium and thallium or indium are maximum in the case of very severe operating conditions, particularly under low pressures, high temperatures and long operating periods.

The following examples illustrate the invention without however limiting the scope thereof.

EXAMPLE 1

The naphtha subjected to the treatment, under conventional operating conditions, has the following characteristics:

______________________________________ASTM distillation 80.degree.-160.degree. C.Composition: aromatic hydrocarbons 7% by weight naphthenic hydrocarbons 27% by weight paraffinic hydrocarbons 66% by weight"Clear research" octane number about 37Average molecular weight 110Specific gravity at 20.degree. C. 0.782______________________________________

This naphtha is passed with recycled hydrogen over two catalysts A and B containing 0.2% of platinum, 0.2% of rhenium, expressed by weight with respect to the carrier consisting of alumina having a specific surface of 240 m.sup.2 /g and a pore volume of 57 cc/g; the chlorine content of catalysts A and B is 1.12%. The catalyst A further contains 0.5% of thallium and the catalyst B further contains 0.5% of indium (expressed by weight with respect to the carrier).

The catalysts A and B have been prepared by adding to 100 g of alumina 100 cc of an aqueous solution containing:

1.90 g of concentrated HCl (d=1.19), 10 g of an aqueous solution of chloroplatinic acid having a 2% platinum content, 8.00 g of a perrhenic acid solution containing 2.5% by weight of rhenium, and 1.06 g of thallium nitrate for catalyst A, or 1.87 g of indium nitrate for catalyst B.

The contact being maintained for 5 hours, the resulting product is dried for 1 hour at 100.degree. C., then roasted at 530.degree. C. in dry air (air dried by means of activated alumina), then reduced with a stream of dry hydrogen (activated alumina) for 2 hours at 450.degree. C. The resulting catalysts A and B contain:

0.2% of platinum 0.2% of rhenium 0.5% of thallium (catalyst A) or 0.5% of indium (catalyst B) 1.12% of chlorine.

The resulting catalysts A and B have a specific surface of 230 m.sup.2 /g and a pore volume of 54 cc/g.

The operating conditions are so selected as to obtain a clear octane number of 96.2.

The conventional mild operating conditions are as follows:

______________________________________pressure 20 barstemperature 490.degree. C.ratio H.sub.2 /hydrocarbon (moles) 5naphtha weight/catalyst weight/hour 3______________________________________

Table I below indicates, for catalysts A and B, the yield of C.sub.5.sup.+ and the hydrogen content of the recycled gas when the desired octane number has been obtained.

TABLE I__________________________________________________________________________ YIELD RECYCLEDCATA- C.sub.5.sup.+ GAS % H.sub.2LYST Metal % B.W. with respect to alumina (weight) (molar)__________________________________________________________________________A 0.2% platinum 0.2% rhenium 0.5% thallium 82.8 82.8B 0.2% platinum 0.2% rhenium 0.5% indium 82.6 82.5__________________________________________________________________________

EXAMPLE 1.A.

(Comparative)

Example 1 is repeated with the use of a catalyst C containing 0.2% of platinum and 0.2% of rhenium, a catalyst D containing 0.2% of platinum and 0.5% of thallium and a catalyst E containing 0.2% of platinum and 0.5% of indium. These catalysts all contain 1.12% of chlorine. The results obtained are slightly lower than those obtained with catalysts A and B, these results being reported in Table II below.

TABLE II__________________________________________________________________________ YIELD RECYCLEDCATA- C.sub.5.sup.+ GAS % H.sub.2LYST Metal % B.W. with respect to alumina (weight) (molar)__________________________________________________________________________C 0.2% platinum 0.2% rhenium - 82.5 82.6D 0.2% platinum - 0.5% thallium 82.5 82.6E 0.2% platinum - 0.5% indium 82.1 82.5__________________________________________________________________________

In fact, the catalysts according to this invention have proved their superiority essentially in a process conducted under severe conditions as shown in example 2.

EXAMPLE 2

The same charge as in example 1 is used to produce a gasoline having a clear octane number of 103. The operating conditions are as follows:

______________________________________pressure 10 barstemperature 530.degree. C.molar ratio H.sub.2 /hydrocarbons 8naphtha weight/catalyst weight/hour 1.65______________________________________

The operation is conducted in the presence of catalysts A and B according to the invention as well as in the presence of various catalysts not conforming with the invention, comprising 1, 2 or 3 metal elements. All the catalysts contain 1.12% of chlorine.

In Table III below are reported the C.sub.5 + yield and the hydrogen content of the recycled gas obtained after 200 hours of run.

The results obtained in this example 2 with the catalysts according to the invention may be maintained over very long time periods of, for example, several months, by operating continuously in a moving bed reactor, the catalyst being withdrawn, for example, in a continuous manner, at a rate so adjusted that the whole catalyst bed of the reactor be progressively renewed by fresh catalyst, for example in about 500 hours.

TABLE III__________________________________________________________________________ C.sub.5.sup.+ RECYCLEDCATA- YIELD GAS % H.sub.2LYST Metal % with respect to the catalyst carrier (weight) (molar)__________________________________________________________________________A 0.2 platinum 0.2 rhenium 0.5 thallium 80.0 79.6F 0.2 platinum -- -- 73.2 72.8C 0.2 platinum 0.2 rhenium -- 76.1 75.3D 0.2 platinum -- 0.5 thallium 76.6 76.1B 0.2 platinum 0.2 rhenium 0.5 indium 79.9 79.5E 0.2 platinum -- 0.5 indium 75.5 75.2G 0.2 platinum 0.2 iridium 0.5 thallium 79.6 78.4H 0.2 platinum 0.08 iridium 0.5 thallium 79.6 78.5I 0.2 platinum 0.2 iridium 0.5 indium 79.5 79.2J 0.2 platinum 0.08 iridium 0.5 indium 79.6 79.2K 0.2 platinum 0.08 iridium -- 75.1 74.8L 0.2 platinum 0.08 ruthenium -- 75.1 74.8M 0.2 platinum 0.2 ruthenium -- 75.0 74.6N 0.2 platinum 0.08 ruthenium 0.5 iron 79.4 78.5O 0.2 platinum 0.08 ruthenium 0.5 rhodium 79.4 78.7P 0.2 platinum 0.08 ruthenium 0.5 manganese 79.5 78.8Q 0.2 platinum -- 0.5 manganese 77.8 77.5R 0.2 platinum 0.08 ruthenium 0.5 gold 79.7 78.7S 0.2 platinum -- 0.5 gold 77.5 77.9T 0.2 platinum 0.08 iridium 0.5 uranium 79.4 78.8U 0.2 platinum 0.08 iridium 0.5 gallium 77.9 77.7__________________________________________________________________________

EXAMPLE 3

Example 2 is repeated with catalysts containing platinum, rhenium, thallium or indium, with varying contents of rhenium, thallium or indium.

The metal contents and the obtained results are reported in Table IV below. All the catalysts contain 1.12% of chlorine.

TABLE IV__________________________________________________________________________ C.sub.5.sup.+ RECYCLEDCATA- Metal % by weight with respect to the YIELD GAS % H.sub.2LYST catalyst carrier (weight) (molar)__________________________________________________________________________A.sub.1 0.2 platinum 0.2 rhenium 0.02 thallium 76.1 75.3A.sub.2 0.2 platinum 0.2 rhenium 0.07 thallium 78.1 77.7A.sub.3 0.2 platinum 0.2 rhenium 0.35 thallium 80.0 79.5A 0.2 platinum 0.2 rhenium 0.5 thallium 80.0 79.6A.sub.4 0.2 platinum 0.2 rhenium 0.7 thallium 78.2 77.7A.sub.5 0.2 platinum 0.2 rhenium 2.5 thallium 77.8 77.4A.sub.6 0.2 platinum 0.2 rhenium 4 thallium 75.5 74.9B.sub.1 0.2 platinum 0.2 rhenium 0.02 indium 76.1 75.3B.sub.2 0.2 platinum 0.2 rhenium 0.07 indium 77.7 77.4B.sub.3 0.2 platinum 0.2 rhenium 0.35 indium 79.8 79.5B 0.2 platinum 0.2 rhenium 0.5 indium 79.9 79.5B.sub.4 0.2 platinum 0.2 rhenium 0.7 indium 77.8 77.4B.sub.5 0.2 platinum 0.2 rhenium 2.5 indium 75.2 74.9B.sub.6 0.2 platinum 0.2 rhenium 4 indium 74.3 73.8V.sub.1 0.2 platinum 0.009 rhenium 0.5 thallium 76.6 76.1V.sub.2 0.2 platinum 0.009 rhenium 0.5 indium 75.5 75.2V.sub.3 0.2 platinum 0.05 rhenium 0.5 thallium 77.8 77.4V.sub.4 0.2 platinum 0.05 rhenium 0.5 indium 76.9 76.2V.sub.5 0.2 platinum 0.30 rhenium 0.5 thallium 77.9 77.4V.sub.6 0.2 platinum 0.30 rhenium 0.5 indium 77.0 76.4V.sub.7 0.2 platinum 3 rhenium 0.5 thallium 75.3 74.5V.sub.8 0.2 platinum 3 rhenium 0.5 indium 74.7 73.6__________________________________________________________________________

Claims

1. A process for reforming hydrocarbons or producing aromatic hydrocarbons at a temperature from 510.degree. to 600.degree. C. under a pressure from 1 to 18 kg/cm.sup.2, at an hourly space velocity of from 1 to 10 volumes of liquid charge per volume of catalyst, the molar ratio hydrogen/hydrocarbon being from 5 to 20, said process being conducted in the presence of a catalyst comprising an alumina carrier and, expressed by weight with respect to alumina:

(a) from 0.05 to 0.6% of platinum,

(b) from 0.01 to 2% of rhenium,

(c) from 0.05 to 3% of thallium or indium, and

(d) from 0.1 to 10% of halogen.

2. A process according to claim 1, said catalyst containing 0.1 to 0.3% of platinum, 0.1 to 0.25% of rhenium and 0.07 to 2% of thallium or indium.

3. A process according to claim 2, said catalyst containing from 0.3 to 0.6% of thallium or indium.

4. A process according to claim 3, said catalyst containing thallium.

5. A process according to claim 3, said catalyst containing indium.

6. A process according to claim 1, wherein the operation is conducted in at least one reaction zone with a moving catalyst bed.

7. A reforming process according to claim 1, whereby a gasoline having a clear octane number of at least 102 is obtained.

8. A process according to claim 1 for reforming hydrocarbons wherein the starting hydrocarbon is a naphtha distilling between about 60.degree. and 220.degree., the average temperature is from about 510.degree. to 580.degree. C. and the pressure is about 5 to 18 kg/cm.sup.2, and the recycle rate is from 6 to 10 moles of hydrogen per mole of charge.

9. A process according to claim 8 wherein the pressure is 6 to 13 kg/cm.sup.2.

10. A process according to claim 1 for producing aromatic hydrocarbons wherein the starting material is a gasoline free of diolefins and mono-olefins, the reaction temperature is 530.degree. to 600.degree., the pressure from 1 to 13 kg/cm.sup.2 and the molar ratio of hydrogen to hydrocarbons is about 6 to 20.

11. A process according to claim 1 wherein the specific surface of the alumina is 50-600 square meters per gram.

12. A process according to claim 1 wherein the specific surface of the alumina is 150-400 meters per gram.

13. A process for reforming hydrocarbons or producing aromatic hydrocarbons at a temperature from 510.degree. to 600.degree. C. under a pressure from 1 to 18 kg/cm.sup.2, at an hourly space velocity of from 1 to 10 volumes of liquid charge per volume of catalyst, the molar ratio hydrogen/hydrocarbon being from 5 to 20, said process being conducted in the presence of a catalyst comprising an alumina carrier and, expressed by weight with respect to alumina:

(a) from 0.05 to 0.6% of platinum,

(b) from 0.01 to 2% of rhenium,

(c) from 0.05 to 3% of thallium, and

(d) from 0.1 to 10% of halogen.

14. A process according to claim 13, said catalyst containing 0.1 to 0.3% of platinum, 0.1 to 0.25% of rhenium and 0.07 to 2% of thallium.

15. A process according to claim 14, said catalyst containing from 0.3 to 0.6% of thallium.

16. A process according to claim 13, wherein the operation is conducted in at least one reaction zone with a moving catalyst bed.

17. A reforming process according to claim 13, whereby a gasoline having a clear octane number of at least 102 is obtained.

18. A process according to claim 13 for reforming hydrocarbons, wherein the starting hydrocarbon is a naphtha distilling between about 60.degree. and 220.degree., the average temperature is from about 510.degree. to 580.degree. C. and the pressure is about 5 to 18 kg/cm.sup.2, and the recycle rate is from 6 to 10 moles of hydrogen per mole of charge.

19. A process according to claim 18, wherein the pressure is 6 to 13 kg/cm.sup.2.

20. A process according to claim 13 for producing aromatic hydrocarbons wherein the starting material is a gasoline free of diolefins and mono-olefins, the reaction temperature is 530.degree. to 600.degree., the pressure from 1 to 13 kg/cm.sup.2 and the molar ratio of hydrogen to hydrocarbons is about 6 to 20.

21. A process according to claim 13, wherein the specific surface of the alumina is 50-600 square meters per gram.

22. A process according to claim 13, wherein the specific surface of the alumina is 150-400 meters per gram.

23. A process for reforming hydrocarbons or producing aromatic hydrocarbons at a temperature from 510.degree. to 600.degree. C. under a pressure from 1 to 18 kg/cm.sup.2, at an hourly space velocity of from 1 to 10 volumes of liquid charge per volume of catalyst, the molar ratio hydrogen/hydrocarbon being from 5 to 20, said process being conducted in the presence of a catalyst consisting essentially of an alumina carrier and, expressed by weight with respect to alumina:

(a) from 0.05 to 0.6% platinum,

(b) from 0.01 to 2% of rhenium,

(c) from 0.05 to 3% of indium, and

(d) from 0.1 to 10% of halogen.

24. A process according to claim 23, said catalyst containing 0.1 to 0.3% of platinum, 0.1 to 0.25% of rhenium and 0.07 to 2% of indium.

25. A process according to claim 24, said catalyst containing from 0.3 to 0.6% of indium.

26. A process according to claim 23, wherein the operation is conducted in at least one reaction zone with a moving catalyst bed.

27. A reforming process according to claim 23, whereby a gasoline having a clear octane number of at least 102 is obtained.

28. A process according to claim 23 for reforming hydrocarbons, wherein the starting hydrocarbon is a naphtha distilling between about 60.degree. to 220.degree., the average temperature is from about 510.degree. to 580.degree. C. and the pressure is about 5 to 18 kg/cm.sup.2, and the recycle rate is from 6 to 10 moles of hydrogen per mole of charge.

29. A process according to claim 28, wherein the pressure is 6 to 13 kg/cm.sup.2.

30. A process according to claim 23 for producing aromatic hydrocarbons wherein the starting material is a gasoline free of diolefins and mono-olefins, the reaction temperature is 530.degree. to 600.degree., the pressure from 1 to 13 kg/cm.sup.2 and the molar ratio of hydrogen to hydrocarbons is about 6 to 20.

31. A process according to claim 23, wherein the specific surface of the alumina is 50-600 square meters per gram.

32. A process according to claim 23, wherein the specific surface of the alumina is 150-400 meters per gram.

33. A process for reforming hydrocarbons or producing aromatic hydrocarbons at a temperature from 510.degree. to 600.degree. C. under a pressure from 1 to 18 kg/cm.sup.2, at an hourly space velocity of from 1 to 10 volumes of liquid charge per volume of catalyst, the molar ratio hydrogen/hydrocarbon being from 5 to 20, said process being conducted in the presence of a catalyst consisting essentially of an alumina carrier and, expressed by weight with respect to alumina:

(a) from 0.05 to 0.6% of platinum,

(b) from 0.01 to 2% of rhenium,

(c) from 0.05 to 3% of thallium, and

(d) from 0.1 to 10% of halogen.

34. A process according to claim 33, said catalyst containing 0.1 to 0.3% of platinum, 0.1 to 0.25% of rhenium and 0.07 to 2% of thallium.

35. A process according to claim 34, said catalyst containing from 0.3 to 0.6% of thallium.

36. A process according to claim 33, wherein the operation is conducted in at least one reaction zone with a moving catalyst bed.

37. A reforming process according to claim 33, whereby a gasoline having a clear octane number of at least 102 is obtained.

38. A process according to claim 33 for reforming hydrocarbons wherein the starting hydrocarbon is a naphtha distilling between about 60.degree. and 220.degree., the average temperature is from about 510.degree. to 580.degree. C. and the pressure is about 5 to 18 kg/cm.sup.2, and the recycle rate is from 6 to 10 moles of hydrogen per mole of charge.

39. A process according to claim 38, wherein the pressure is 6 to 13 kg/cm.sup.2.

40. A process according to claim 33 for producing aromatic hydrocarbons wherein the starting material is a gasoline free of diolefins and mono-olefins, the reaction temperature is 530.degree. to 600.degree., the pressure from 1 to 13 kg/cm.sup.2 and the molar ratio of hydrogen to hydrocarbons is about 6 to 20.

41. A process according to claim 33, wherein the specific surface of the alumina is 50-600 square meters per gram.

42. A process according to claim 33, wherein the specific surface of the alumina is 150-400 meters per gram.