Alkylation catalyst for C.sub.4 -C.sub.5 isoparaffins using at least one C.sub.2 -C.sub.6 olefin

Abstract

The present invention concerns a catalyst comprising a porous organic or mineral support, preferably silica, and an acidic phase containing B(OSO.sub.2 CF.sub.3).sub.3 and at least one acid selected from the group formed by sulphuric acid (H.sub.2 SO.sub.4) and trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H), the support having been impregnated by said acidic phase, said catalyst being such that it is constituted essentially by particles with an average diameter of between 0.1 and 150 .mu.m, such that the support, prior to its impregnation with said acidic phase, has a total pore volume of between 0.5 and 6 cm.sup.3 per gram and said catalyst being characterized in that said acidic phase contains:between 0.1 and 70% by weight of B(OSO.sub.2 CF.sub.3).sub.3 ;between 0 and 90% by weight of H.sub.2 SO.sub.4 ;between 0 and 90% by weight of CF.sub.3 SO.sub.3 H.The catalyst is useful for the catalytic alkylation of isobutane and/or isopentane in the presence of at least one olefin containing 2 to 6 carbon atoms per molecule, preferably 3 to 6 carbon atoms per molecule.

Description

BACKGROUND OF THE INVENTION

The present invention concerns a catalyst comprising a porous organic or mineral support, preferably silica, and an acidic phase containing B(OSO.sub.2 CF.sub.3).sub.3 and at least one acid selected from the group formed by sulphuric acid (H.sub.2 SO.sub.4) and trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H), said support having been impregnated with said acidic phase. The invention also concerns the preparation and use of the catalyst for the catalytic alkylation of an isoparaffin (isobutane and/or isopentane) in the presence of at least one olefin containing 2 to 6 carbon atoms per molecule.

It is particularly important for spark ignition internal combustion engines, in particular those with high compression ratios, to use fuels with high octane numbers, i.e., essentially constituted by highly branched paraffin hydrocarbons. Alkylation of isoparaffins (isobutane and/or isopentane) by olefins containing 3 to 6 carbon atoms per molecule can produce such products. This reaction requires the use of highly acidic catalysts, primarily to reduce side reactions such as hydride abstraction from the olefin and polymerisation, which produces less branched hydrocarbons with low octane numbers and unsaturated hydrocarbons, also cracking reactions and dismutation reactions.

Existing processes for the production of hydrocarbons by alkylation of isobutane with olefins generally use either sulphuric acid or hydrofluoric acid as a catalyst. In these processes, the acidic catalyst constitutes a liquid phase which is brought into contact with the liquid isobutane-olefin mixture to form an emulsion. These processes are costly and pose substantial problems as regards personnel and environmental safety. In order to overcome these problems, catalytic systems other than those using liquid phase sulphuric acid and hydrofluoric acid have been sought.

To catalyse the alkylation of isoparaffins by olefins, acidic catalysts have been proposed which use a number of acidic solids of different natures, such as molecular sieves, macroreticular resins which may be combined with BF.sub.3, Lewis acids and/or Bronsted acids deposited on a variety of inorganic supports, chlorinated aluminas, graphites with intercalated Lewis and/or Bronsted acids, and anions deposited on oxide supports such as ZrO.sub.2 /SO.sub.4. These solids produce branched isoparaffins but suffer from a number of major defects, among them the use of isobutane/olefin molar ratios which are often very high to limit secondary reactions, and low stability of catalytic activity with time (inhibition of the catalyst by deposition of unsaturated oligomers), requiring frequent regeneration. Further, the low acidity of certain acidic solids, such as molecular sieves, requires the use of high reaction temperatures which inhibit the production of hydrocarbons with high octane numbers.

European patent application EP-A-0 539 277 describes a catalyst containing silica and a solid acidic phase comprising sulphuric acid, the silica of that application having a pore volume of between 0.005 and 1.5 cm.sup.3 /g, and a specific surface area of between 0.01 and 1500 m.sup.2 /g. The acidic phase optionally includes an additive selected from the group formed by H.sub.3 PO.sub.4, B(OH).sub.3, BF.sub.4 H, FSO.sub.3 H, CF.sub.3 CO.sub.2 H, SbF.sub.5, CF.sub.3 SO.sub.3 H and SO.sub.3.

European patent application, EP-A-0.623.388 describes a catalyst comprising an organic or mineral porous support and a mixture constituted by sulphuric acid, trifluoromethane sulphonic acid and, optionally, water.

SUMMARY OF THE INVENTION

The present invention concerns a catalyst comprising a porous organic or mineral support, preferably silica, and an acidic phase comprising B(OSO.sub.2 CF.sub.3).sub.3 and at least one acid from the group formed by sulphuric acid (H.sub.2 SO.sub.4) and trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H), said support having been impregnated with said acidic phase, said catalyst being such that it is essentially constituted by particles with an average diameter of between 0.1 and 150 .mu.m (1 .mu.m=10.sup.-6 m), preferably between 5 and 110 .mu.m, more preferably between 5 and 80 .mu.m, such that its content by weight of acidic phase is greater than 40%, preferably greater than 70%, such that the support, prior to its impregnation with said acidic phase, has a total porous volume of between 0.5 and 6 cm.sup.3 per gram, preferably between 0.6 and 6 cm.sup.3 per gram, more preferably between 1.5 and 6 cm.sup.3 per gram, and said catalyst being characterised in that said acidic phase comprises:

between 0.1 and 70% by weight, preferably between 0.2 and 65% by weight, of B(OSO.sub.2 CF.sub.3).sub.3 ; between 0 and 90% by weight, preferably between 0 and 80% by weight, of H.sub.2 SO.sub.4 ; between 0 and 90% by weight, preferably between 0 and 85% by weight, of CF.sub.3 SO.sub.3 H.

The invention also concerns the preparation and use of said catalyst for the catalytic alkylation of at least one isoparaffin selected from the group formed by isobutane and isopentane (i.e., isobutane and/or isopentane: isobutane, or isopentane, or isobutane and isopentane) in the presence of at least one olefin containing 2 to 6 carbon atoms per molecule, preferably 3 to 6 carbon atoms per molecule.

The catalyst of the present invention surprisingly produces improved catalytic performances compared with those described in European patent application EP-A-0.539.277 and in European patent application EP-A-0.623.388.

The concentration of sulphuric acid is advantageously between 90% and 100% by weight, preferably between 97% and 100% by weight, more preferably between 98% and 100% by weight.

The concentration of trifluoromethane sulphonic acid is advantageously between 95% and 100% by weight, preferably between 98% and 100% by weight.

The weight content of the acidic phase in the catalyst is generally greater than 40%, preferably greater than 70%.

The B(OSO.sub.2 CF.sub.3).sub.3 in the acidic phase of the catalyst of the invention is prepared using methods which are known to the skilled person. By way of non limiting example, preferred methods which can be mentioned are firstly, reacting a boron trihalide BX.sub.3 (where X is a halogen, preferably Cl or Br) with 3 molar equivalents of trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H) in the reaction:

BX.sub.3 +3 CF.sub.3 SO.sub.3 H.fwdarw.B(OSO.sub.2 CF.sub.3).sub.3 +3 HX

The second preferred method of the invention consists in reacting one mole of boron trihalide BX.sub.3 (where X is a halogen, preferably Cl or Br) with 3 molar equivalents of silver trifluoromethane sulphonate CF.sub.3 SO.sub.3 Ag:

BX.sub.3 +3 CF.sub.3 SO.sub.3 Ag.fwdarw.B(OSO.sub.2 CF.sub.3).sub.3 +3 AgX

The two above reactions,, exemplifying the first and second preferred methods of the invention, are described in particular by Engelbrecht et al, in Z Anorg Chem, 1977, 433, 19, and by G A Olah et al, in J Org Chem, 1984, 49, 4591-4594.

When using silica as the support, it can contain impurities such as oxides, alkalis, alkaline-earths, aluminium compounds or any other impurity known to the skilled person, the total quantity of these impurities generally not exceeding 2% by weight with respect to the silica.

The organic or mineral porous support, preferably silica, is generally such that, before impregnation by the acidic phase, the specific surface area is between 0.1 and 1500 m.sup.2 /g, and its total pore volume is between 0.5 and 6 cm.sup.3 /g, preferably between 0.6 and 6 cm.sup.3 /g, more preferably between 1.5 and 6 cm.sup.3 /g. In addition, it is generally essentially constituted by particles with an average diameter of between 0.1 and 150 .mu.m, preferably between 5 and 110 .mu.m, more preferably between 5 and 80 .mu.m.

The weight content of the acidic phase in the catalyst is generally more than 40%, preferably more than 70%.

The acidic phase generally occupies between 80% and 100% of the total pore volume of the support, preferably between 90% and 100% of the pore volume.

The preparation process for the catalyst of the invention comprises two steps. In the first step, the porous organic or mineral support is calcined at a temperature of more than 50.degree. C., preferably more than 80.degree. C., more preferably between 150.degree. C. and 600.degree. C., for example at about 500.degree. C. This calcining step usually lasts between 10 minutes and 50 hours, preferably between 15 minutes and 25 hours. Calcining is generally carried out in the presence of dry air or a dry air/nitrogen mixture at a flow rate of between 0.001 and 10 l/h/g, preferably between 0.1 and 5 l/h/g. The second step consists of impregnating the calcined support with the acidic phase. This step can be effected using any technique known to the skilled person. An acidic phase preparation step can be added to this preparation method, prior to the impregnation step.

The catalyst of the present invention is used in a process in which the alkylation reaction of isobutane by olefins is carried out under improved conditions. In particular, since the reaction is characterised by high exothermicity (about 83.6 kJ/mole of butene transformed if the olefin is butene and if the isoparaffin is isobutane), the use of the catalyst of the invention produces good temperature homogeneity and reactant concentration.

The operating conditions, in particular the temperature and pressure in the isobutane alkylation process using the catalyst of the present invention, are generally selected so that the mixture, constituted by the isoparaffin, olefin(s) and reaction products, is liquid. In addition, it is important that the catalyst is immersed in the liquid to ensure good liquid-solid contact.

The catalyst of the invention is advantageously used in the isobutane and/or isopentane alkylation reaction zone with at least one olefin containing 2 to 6 carbon atoms per molecule, preferably 3 to 6 carbon atoms per molecule, in the liquid phase and mixed with the isoparaffin and/or isoparaffin mixture. The catalyst of the invention can be used in an expanded bed, in an almost ideally agitated reaction zone or in a circulating bed, preferably in a process using a continuous liquid phase, the catalyst being used in the form of a suspension in the two operative embodiments described below.

In a first preferred operating embodiment for the catalyst of the invention, a reaction zone using almost perfect mixing is used, i.e., a perfect mix or a near perfect mix (agitated or Grignard vessel), using at least one agitation means, for example at least one propeller, to obtain sufficient agitation of the catalyst in suspension in the liquid hydrocarbon phase, this phase generally including the isoparaffin (isobutane and/or isopentane), at least one olefin, optionally at least one inert diluent (for example propane and n-butane) and the alkylation reaction products. The feed to be converted, constituted by isobutane and/or isopentane and at least one olefin, can for example be introduced in the liquid form at at least one point into the liquid hydrocarbon phase present in the reaction zone.

In a second preferred operating embodiment, the catalyst of the invention in suspension in the hydrocarbon phase is a mobile bed in co-current mode, i.e., a circulating bed. In this embodiment, the catalyst in suspension in the hydrocarbon liquid phase generally including the isoparaffin (isobutane and/or isopentane), at least one olefin, optionally at least one inert diluent (for example propane or n-butane) and the alkylation reaction products, circulates from bottom to top in the reaction zone. The assembly constituted by the catalyst suspension in the hydrocarbon phase then circulates through at least one heat exchanger and at least one pump before being reintroduced to the inlet to the reaction zone. The feed to be converted, constituted by isobutane and/or isopentane and at least one olefin, is introduced either in the liquid form, or in the gaseous state at at least one point of the reaction zone.

In the two types of embodiment described above, the isoparaffin (isobutane and/or isopentane) which is either unconverted or has been introduced in excess with respect to the stoichiometry of the reaction, is generally recycled after separation of the alkylate, either by direct introduction into the reaction zone, or by mixing with the feed to be converted.

The isoparaffin-olefin mixture is generally introduced into the reaction zone at an hourly space velocity, expressed as the weight of olefin introduced per unit weight of catalyst per hour (pph), of between 0.001 and 10 h.sup.-1, preferably between 0.002 and 2 h.sup.-1. Mixing can also be effected within the reaction zone. In all cases, the mixture thus constituted is in the reaction zone under temperature and pressure conditions in which the hydrocarbon mixture remains liquid on the catalyst.

The reaction temperature is generally less than +10.degree. C., preferably 0.degree. C. and more preferably less than -3.degree. C. The pressure in the reaction zone is generally sufficient to maintain the hydrocarbons in the liquid state in this zone.

In order to limit secondary reactions, an excess of isoparaffin over olefin can be used. By way of example, in the case of alkylation of isobutane by a butene, the isobutane can be introduced pure into the feed or in the form of a mixture of butanes containing, for example, at least 40% of isobutane. A pure butene or a mixture of butene isomers can also be introduced. In all cases, the molar ratio of isobutane/butene(s) in the feed is generally between 1 and 100, preferably between 3 and 50 and more preferably between 5 and 15.

The reaction products can be regularly monitored by measurement of the bromine index, for example using the method described in French Standard Pr.M 07.071, March 1969.

When the catalyst and the reaction conditions are carefully selected (in particular the temperature), the catalyst of the invention produces products of the alkylation of at least one isoparaffin by at least one olefin which are of importance as engine fuels and petrol constituents and which contain, for example, at least 60 mole % of paraffins containing 8 carbon atoms per molecule and less than 1 mole % of unsaturated compounds, the paraffins containing 8 carbon atoms per molecule containing 70 to 98 mole % of trimethylpentanes.

A further advantage of the catalyst of the present invention is the possibility of alkylating isobutane at low temperature, with mixtures of olefins containing 3 to 6 carbon atoms per molecule, where the proportion of olefins containing more than 4 carbon atoms per molecule is very high.

THE FOLLOWING EXAMPLES ILLUSTRATE THE INVENTION WITHOUT IN ANY WAY LIMITING ITS SCOPE.

EXAMPLE 1

Preparation of Catalyst 1: in Accordance with the Invention

16 g of macroporous silica with a specific surface area of 395 m.sup.2 /g, a total pore volume of 2.4 cm.sup.3 /g and an average particle diameter of 45 .mu.m was activated by calcining in air for 4 hours at 500.degree. C. The activated silica was stored under argon. 14 g of the dehydrated silica was then dry impregnated, protected from moisture, with 50 g of a mixture constituted by:

37.4 g of a solution containing 99 weight % of H.sub.2 SO.sub.4 and 1 weight % of water, 6.6 g of a solution containing 6.46 g of CF.sub.3 SO.sub.3 H acid and 0.14 g of water, 6 g of B(OSO.sub.2 CF.sub.3).sub.3.

The composition by weight of the acidic phase was as follows:

______________________________________ H.sub.2 SO.sub.4 74.05% CF.sub.3 SO.sub.3 H 12.92% B(OSO.sub.2 CF.sub.3).sub.3 12.00% H.sub.2 O 1.03%______________________________________

The solid obtained, catalyst 1, had an acidic phase concentration of 78.1 weight %; it was stored under argon at -18.degree. C.

Alkylation of Isobutane by But-1-ene with Catalyst 1

Catalyst 1 was used to alkylate isobutane with but-1-ene to produce branched paraffins with high octane numbers. 36 g of catalyst 1, prepared as above, was introduced into a glass Fischer & Porter reactor with a volume of 360 ml which had been purged with argon. The reactor containing the catalyst was then sealed, placed under low vacuum, then cooled to a temperature of -20.degree. C.

100 cm.sup.3 of isobutane was then added to the reactor containing the catalyst, with stirring, the reactor being immersed in a cold bath at -6.degree. C. The catalyst+isobutane system was stirred for 30 minutes to homogenise the temperature.

A mixture of isobutane and but-1-ene containing 20 weight % of but-1-ene was continuously added, over a period of 8 hours, the temperature of the reactor being held at -5.degree. C. for the whole of the injection period. The volume flow rate of the but-1-ene was 25 ml/h.

After reaction, the hydrocarbon phase was extracted from the reactor, then the isobutane was slowly evaporated and the alkylate was recovered and analysed by vapour phase chromatography. The composition by weight is given in Table 1. 100% of the olefin was converted.

EXAMPLE 2

Preparation of Catalyst 2, Not in Accordance with the Invention

14 g of dehydrated silica was prepared in identical fashion to that described for the preparation of the catalyst in accordance with the invention. 14 g of the silica was then dry impregnated, protected from moisture, with 50 g of a mixture constituted by:

42.5 g of a solution containing 99 weight % of H.sub.2 SO.sub.4 and 1 weight % of water, 7.5 g of a solution containing 7.35 g of CF.sub.3 SO.sub.3 H acid and 0.15 g of water,

The composition by weight of the acidic phase was as follows:

______________________________________ H.sub.2 SO.sub.4 84.15% CF.sub.3 SO.sub.3 H 14.68 H.sub.2 O 1.17%______________________________________

The solid obtained, catalyst 2, had an acidic phase concentration of 78.1 weight %; it was stored under argon at -18.degree. C.

Alkylation of Isobutane by But-1-ene with Catalyst 2

Catalyst 2 was used to alkylate isobutane with but-1-ene to produce branched paraffins with high octane numbers. 36 g of catalyst 2, prepared as above, was introduced into a glass Fischer & Porter reactor with a volume of 360 ml which had been purged with argon. The reactor containing the catalyst was then sealed, placed under low vacuum, then cooled to a temperature of -20.degree. C.

100 cm.sup.3 of isobutane was then added to the reactor containing the catalyst, with stirring, the reactor being immersed in a cold bath at -6.degree. C. The catalyst+isobutane system was stirred for 30 minutes to homogenise the temperature.

A mixture of isobutane and but-1-ene containing 20 weight % of but-1-ene was continuously added, over a period of 8 hours, the temperature of the reactor being held at -5.degree. C. for the whole of the injection period. The volume flow rate of the but-1-ene was 10 ml/h.

After reaction, the hydrocarbon phase was extracted from the reactor, then the isobutane was slowly evaporated and the alkylate was recovered and analysed by vapour phase chromatography. The composition by weight is given in Table 1. 100% of the olefin was converted.

TABLE 1______________________________________ CATALYST 1 CATALYST 2 Example 1 Example 2______________________________________C.sub.5 -C.sub.7 2.1 2.5C.sub.8 total 94.1 93C.sub.9.sup.+ 3.8 4.5______________________________________

Table 1 shows the effect of the presence of B(OSO.sub.2 CF.sub.3).sub.3 in the catalyst. Catalyst 1, in accordance with the invention, produced a higher selectivity towards C.sub.8 compounds than that obtained in the presence of catalyst 2 for a but-1-ene flow rate of two and a half times the size of that used to test catalyst 2 which is not in accordance with the invention,. Catalyst 1, in accordance with the invention, is thus more active and more selective than catalyst 2.

EXAMPLE 3

Preparation of Catalyst 3, in Accordance with the Invention

15 g of silica with a total pore volume of 2.2 cm.sup.3 /g, a specific surface area of 420 m.sup.2 /g and an average particle diameter of 60 .mu.m was activated by drying at 150.degree. C. for 12 hours. The activated silica was stored under nitrogen. 10 g of the dehydrated silica was then dry impregnated, protected from moisture, with 40.5 g of a mixture constituted by:

33.2 g of a H.sub.2 SO.sub.4 solution containing 100 weight % of H.sub.2 SO.sub.4, 7.3 g of B(OSO.sub.2 CF.sub.3).sub.3.

The composition by weight of the acidic phase was as follows:

______________________________________ H.sub.2 SO.sub.4 82.0% B(OSO.sub.2 CF.sub.3).sub.3 18.0%______________________________________

The solid obtained, catalyst 3, had an acidic phase concentration of 80.2 weight %; it was stored under argon at -18.degree. C.

Alkylation of Isobutane by But-1-ene with Catalyst 3

20 g of catalyst 3, prepared as above, was introduced into a glass Fischer & Porter reactor with a volume of 360 ml which had been purged with argon. The reactor containing the catalyst was then sealed, placed under low vacuum, then cooled to a temperature of -20.degree. C.

150 cm.sup.3 of isobutane was then added to the reactor containing the catalyst, with stirring (propeller), the reactor being immersed in a cold bath at -5.degree. C. The catalyst 3+isobutane system was stirred for 30 minutes to homogenise the temperature.

6.1 g per hour of but-1-ene was added steadily, over a total period of 6 hours, the temperature of the reactor being held at -5.degree. C. for the whole of the injection period.

After reaction, the hydrocarbon phase was extracted from the reactor, then the isobutane was slowly evaporated and the alkylate was recovered and analysed by vapour phase chromatography. The composition by weight is given in Table 2. 100% of the olefin was converted.

EXAMPLE 4

Preparation of Catalyst 4, Not in Accordance with the Invention

10 g of dehydrated silica, identical to that used in Example 3, was prepared in identical fashion to the catalyst of the invention described in Example 3. 10 g of the silica was then dry impregnated, protected from moisture, with 40.5 g of 100 weight % H.sub.2 SO.sub.4.

The solid obtained, catalyst 4, had an acidic phase concentration of 80.2 weight %; it was stored under argon at -18.degree. C.

Alkylation of Isobutane by But-1-ene with Catalyst 4

20 g of catalyst 4, prepared as above, was introduced into a glass Fischer & Porter reactor with a volume of 360 ml which had been purged with argon. The reactor containing the catalyst was then sealed, placed under low vacuum, then cooled to a temperature of -20.degree. C.

150 cm.sup.3 of isobutane was then added to the reactor containing the catalyst, with stirring (propeller), the reactor being immersed in a cold bath at -5.degree. C. The catalyst 4+isobutane system was stirred for 30 minutes to homogenise the temperature.

6.1 g per hour of but-1-ene was added steadily, over a total period of 6 hours, the temperature of the reactor being held at -5.degree. C. for the whole of the injection period.

After reaction, the hydrocarbon phase was extracted from the reactor, then the isobutane was slowly evaporated and the alkylate was recovered and analysed by vapour phase chromatography. The composition by weight is given in Table 2. 100% of the olefin was converted.

TABLE 2______________________________________ CATALYST 3 CATALYST 4 Example 3 Example 4______________________________________C.sub.5 -C.sub.7 3.3 8.7C.sub.8 total 92.5 80.5C.sub.9.sup.+ 4.2 10.8______________________________________

Table 2 shows the effect of the presence of B(OSO.sub.2 CF.sub.3).sub.3 in the catalyst. Catalyst 3, in accordance with the invention, produced a higher selectivity towards C.sub.8 compounds than that obtained in the presence of catalyst 4 for the same but-1-ene flow rate. Catalyst 3, in accordance with the invention, is thus more active and more selective than catalyst 4.

EXAMPLE 5

Preparation of Catalyst 5, in Accordance with the Invention

15 g of silica with a total pore volume of 2.2 cm.sup.3 /g, a specific surface area of 420 m.sup.2 /g and an average particle diameter of 60 .mu.m was activated by drying at 150.degree. C. for 12 hours. The activated silica was stored under nitrogen. 10 g of the dehydrated silica was then dry impregnated with 40.5 g of a mixture constituted by:

33.1 g of a solution containing 100 weight % of CF.sub.3 SO.sub.3 H, 7.3 g of B(OSO.sub.2 CF.sub.3).sub.3.

The composition by weight of the acidic phase was as follows:

______________________________________ CF.sub.3 SO.sub.3 H 81.9% B(OSO.sub.2 CF.sub.3).sub.3 18.1%______________________________________

The solid obtained, catalyst 5, had an acidic phase concentration of 80.2 weight %; it was stored under argon at -18.degree. C.

Alkylation of Isobutane by But-1-ene with Catalyst 5

20 g of catalyst 5, prepared as above, was introduced into a glass Fischer & Porter reactor with a volume of 360 ml which had been purged with argon. The reactor containing the catalyst was then sealed, placed under low vacuum, then cooled to a temperature of -20.degree. C.

150 cm.sup.3 of isobutane was then added to the reactor containing the catalyst, with stirring (propeller), the reactor being immersed in a cold bath at -5.degree. C. The catalyst 5+isobutane system was stirred for 30 minutes to homogenise the temperature.

8 g of but-1-ene per hour was added steadily, over a total period of 6 hours, the temperature of the reactor being held at -5.degree. C. for the whole of the injection period.

After reaction, the hydrocarbon phase was extracted from the reactor, then the isobutane was slowly evaporated and the alkylate was recovered and analysed by vapour phase chromatography. The composition by weight is given in Table 3. 100% of the olefin was converted.

TABLE 3______________________________________ CATALYST 5 Example 5______________________________________ C.sub.5 -C.sub.7 4.3 C.sub.8 total 89.1 C.sub.9.sup.+ 6.6______________________________________

Claims

1. A catalyst comprising a porous organic or mineral support and an acidic phase comprising B(OSO.sub.2 CF.sub.3).sub.3 and at least one acid from the group consisting of sulphuric acid (H.sub.2 SO.sub.4) and trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H), said support having been impregnated with said acidic phase, said catalyst being consisting essentially of particles having an average diameter of between 0.1 and 150 .mu.m, said support, prior to its impregnation with said acidic phase, having a total pore volume of between 0.5 and 6 cm.sup.3 per gram, and said catalyst being characterized in that the content of said acidic phase in the catalyst is greater than 40% by weight and said acidic phase comprises:

between 0.1 and 70% by weight of B(OSO.sub.2 CF.sub.3).sub.3 ;

between 0 and 90% by weight of H.sub.2 SO.sub.4 ;

between 0 and 90% by weight of CF.sub.3 SO.sub.3 H, with the provision that the total of H.sub.2 SO.sub.4 and CF.sub.3 SO.sub.3 H is above zero.

2. A catalyst according to claim 1, consisting essentially of particles with an average diameter of between 5 and 110 .mu.m.

3. A catalyst according to claim 1, such that the support, prior to its impregnation with said acidic phase, has a total pore volume of between 0.6 and 6 cm.sup.3 per gram.

4. A catalyst according to claim 1, such that the support, prior to its impregnation with said acidic phase, has a total pore volume of between 1.5 and 6 cm.sup.3 per gram.

5. A catalyst according to claim 1 such that the content by weight of said acidic phase is greater than 70%.

6. A catalyst according to claim 1, in which said support is silica.

7. The preparation of a catalyst according to claim 1, comprising at least two steps, in which in the first step the support is calcined at a temperature of more than 50.degree. C. for a period of between 10 minutes and 50 hours, and in the second step said calcined support is impregnated with said acidic phase.

8. Preparation according to claim 7, in which the B(OSO.sub.2 CF.sub.3).sub.3 is obtained using one of methods (a) or (b) as follows:

a) reacting a boron trihalide BX.sub.3 (where X is a halogen) with 3 molar equivalents of trifluoromethane sulphonic acid (CF.sub.3 SO.sub.3 H) in accordance with the reaction:

BX.sub.3 +3 CF.sub.3 SO.sub.3 H.fwdarw.B(OSO.sub.2 CF.sub.3).sub.3 +3 HX

b) reacting one mole of boron trihalide BX.sub.3 (where X is a halogen) with 3 molar equivalents of silver trifluoromethane sulphonate CF.sub.3 SO.sub.3 Ag:

BX.sub.3 +3 CF.sub.3 SO.sub.3 Ag.fwdarw.B(OSO.sub.2 CF.sub.3).sub.3 +3 AgX.

9.

9. In a process for the catalytic alkylation of at least one isoparaffin selected from the group consisting of isobutane and isopentane in the presence of at least one olefin containing 2 to 6 carbon atoms per molecule, the improvement comprising employing as a catalyst the composition according to claim 1, and conducting the alkylation at a temperature of less than +10.degree. C. and under sufficient pressure to maintain hydrocarbon alkylation reactants and products in the liquid phase.

10. A catalyst according to claim 1, wherein the acidic phase contains zero CF.sub.3 SO.sub.3 H.

11. A catalyst according to claim 1, wherein the acidic phase contains zero H.sub.2 SO.sub.4.

12. A catalyst according to claim 1, wherein the acidic phase contains both CF.sub.3 SO.sub.3 H and H.sub.2 SO.sub.4.

13. A catalyst produced according to claim 7.

14. A process according to claim 9, wherein the alkylation temperature is less than 0.degree. C.

15. A process according to claim 9, wherein the alkylation temperature is less than -3.degree. C.

16. A catalyst according to claim 12, wherein the support is silica.

17. A catalyst according to claim 12, wherein the support is silica and the composition of the acidic component in the acid phase is, by weight, about 12% B(OSO.sub.2 CF.sub.3).sub.3, about 74% H.sub.2 SO.sub.4, and about 13% CF.sub.3 SO.sub.3 H.

18. In a process for the catalytic alkylation of at least one isoparaffin selected from the group consisting of isobutane and isopentane in the presence of at least one olefin containing 2 to 6 carbon atoms per molecule, the improvement comprising employing as a catalyst the composition according to claim 17, and conducting the alkylation at a temperature of less than +10.degree. C. and under sufficient pressure to maintain hydrocarbon alkylation reactants and products in the liquid phase.

19. A catalyst according to claim 1, wherein the acid phase consists essentially of B(OSO.sub.2 CF.sub.3).sub.3 and at least one of H.sub.2 SO.sub.4 and CF.sub.3 SO.sub.3 H.

20. A catalyst according to claim 12, wherein the acid phase consists essentially of B(OSO.sub.2 CF.sub.3).sub.3, H.sub.2 SO.sub.4 and CF.sub.3 SO.sub.3 H.