PROCESS AND APPARATUS FOR PREPARING HETEROGENEOUS CATALYSTS

Abstract: The invention relates to a process and to an apparatus for preparing a heterogeneous catalyst having at least one catalytically active species bound to the surface of a support material. According to the process, the surface of the support (6) is first pretreated. A catalyst reagent containing the catalytically active species or its precursor is vaporised and the vapour is routed into a reaction chamber (6) where it is brought to interact with the support material. The catalyst reagent not bound to the support is withdrawn from the reaction chamber (4) in gaseous form. If necessary, the species bound to the support is post-treatead in order to convert it into a catalytically active form. According to the invention, the amount of catalyst reagent brought into the reaction chamber is at least equal to, preferably in excess of the number of available binding sites on the surface (6). The temperature of the support is kept higher than the condensation temperature of the vapour and at the same time at a sufficiently high level to attain the thermal activation energy needed for forming bonds between the active species and the support. By binding the catalytically active species in this way to the support, it is possible to provide a heterogeneous catalyst having a high activity even at small amounts of the active species.

Description: Process and apparatus for preparing heterogeneous catalys The present invention relates to a process according to t preamble of claim 1, for preparing a heterogeneous cataly comprising a support and at least one catalytically activ species bound to its surface. According to such a process, the surface of the support is optionally first pretreated. The catalyst reagent containi the catalytically active species or its precursor is vapo ized and the vapour is conducted to a reaction chamber wh it is contacted with the support. The catalyst reagent not bound to the support is then withdrawn in gaseous form fr the reaction chamber. If necessary, the species bound to support is posttreated in order to convert it into a cata¬ lytically active form. The invention also relates to an apparatus according to t preamble of claim 15, for preparing heterogeneous catalyst As far as the prior art is concerned, reference is made to the following publications: 1. GB Patent Specification No. 1,105,564 (1968) 2. US Patent Specification No. 4,262,102 (1981) 3. US Patent Specification No. 4,362,654 (1982) 4. US Patent Specification No. 4,380,616 (1983) 5. Kase, A., Asa ura, K., Egawa, C. and Iwasawa, Y., New Pd/Ultra-Thin Amorphous-Oxide Layer/ZSM-5 Catalysts for Selective Formation of Propane from CO/H2. Chem. Lett. 6 (1986) 855-858 6. Asakura, K. and Iwasawa, Y., The Surface Structure and Catalytic Properties of One Atomic Layer Amorphous Niobium Oxide Attached on Silicon Dioxide, Chem. Lett. 6 (1986) 859-862 7. Asakura, K. and Iwasawa, Y., New Reversible Enhencemen Depression Phenomenon on Catalysis of Platinum Support on One Atomic Layer Niobium Oxide for Ethane Hydro- genation, Chem. Lett. 4 (1988), 633-636 8. Asakura, K, Aoki., M. and Iwasawa, Y, Selective Isopen Formation from CH3OH on a New One Atomic Layer Zrθ2/ZS Hybrid Catalyst, Catalysis Lett. 1(1988), 395-404 9. McDaniel, M.P., The State of Cr(VI) on the Phillips Polymersation Catalyst II: The Reaction between Silica and Crθ2Cl2 Journal of Catalysis 76 (1982) 17-28 10. US Patent Specification No. 4,439,543 (1984) Traditionally, heterogeneous catalysts have been prepared depositing catalytically active compounds from the liquid phase onto the surface of the support by means of impregna ion, precipitation or ion exchange. The starting materials used here comprise chemical compounds, often salts, which are soluble in known solvents. The solvents most frequentl employed are water and different alcohols. One drawback of the conventional technology is the large number of stages involved in catalyst preparation. The preparation of catalysts is recognised as an extremely delicate procedure requiring very accurate control of each requisite stage of the process. Another drawback of prior art methods is associated with t need for solvents. The solvents by themselves often react with the support causing changes to the surface structure. This is particularly the case with the use of zeolites as the support material. The acidity of the surface has a decisive effect on the activity of the catalyst. The acidi is influenced both by the type of the acid sites, for example, the Brϋnstedt and Lewis type, as well as by the number of sites. The acid sites can be influenced by, e.g., different heat treatments, hen zeolites are treated with solvents, especially water, after a heat treatment, a definite change in the distribution of the acid sites is discernible. At least some of the acid sites then assume reversibly different forms. Thus, it is clear that the degree of acidity cannot be controlled during impregnatio or ion exchange. In addition to the above-mentioned drawbacks, the solvent used are often contaminated with impurities that can adversely affect the activity of the catalyst. In order to eliminate the cited drawbacks of the liquid phase preparation processes, a number of different gas ph processes have been developed. Reference [1] outlines a process that involves heating rhenium heptoxide to a temperature in the range from 150° 700 β C and allowing the vapour to condense on the surface of an aluminium oxide support which is maintained at a temperature below 50*C. Alternatively, the reaction is carried out at a temperature between 500 β and 600 β C, the Rβ2θ7 partially decomposing to rhenium metal and forming metal deposition on the alumina. The citation includes an example disclosing the preparation of a catalyst containi In the following three references [2, 3 and 4], processes preparing silica-supported chromium catalysts have been described. The US Patent Specification No. 4,262,102 pres a method that involves vaporizing elemental chromium by heating it to a temperature of from 1400° to 1700'C in a high vacuum metal evaporator, the chromium sublimating fr the vapour phase on a chilled support in the form of smal particles [2] . The procedures described in US Patent Specifications Nos. 4,362,654 and 4,380,616 comprise plac the silica support and a piece of chromium metal in a rou bottomed flask, evacuating the flask, and stirring the silica in the flask with a magnetic stirrer. The chromium vaporized by heating with heat resistances [3 and 4]. In this case also, the chromium adheres to the support surface in the form of small particles. in processes of the above type, the dispersion of the activ metal may be heterogenic and there is not yet a proper understanding of how the carbene complex is formed on the catalyst. in the Department of Chemistry at Tokyo University, reasearchers have prepared different catalysts having extremely thin layers, known as "atomic layers", of metal oxide bound to the surface of the supports [5 - 8] . Ideally the catalysts comprises 1 to 3 of these atomic layers. Reference [5] discloses the preparation of catalysts having ultra-thin Lβ2θ3, Tiθ2 Siθ2, and Nb2θs layers on the outer surface of a zeolite (ZSM-5). Reference [6] describes the corresponding catalysts having a Siθ2 support. According to reference [5], catalysts containing Siθ2 and Tiθ2 are prepared by contacting methyltriethoxysilane and titanium isopropoxide vapors with the hydroxyls of ZSM-5 surfaces at 473 K (200 β C) in a vacuum. Similarly, the Zr0 2 /ZSM-5 hybrid catalyst was prepared by contacting vaporized Zr tetraoxide having a vapour pressure of 133 Pa at 473 K with ZSM-5 at the same temperature. By repeating the binding reaction about 3 times, in both cases a single atom oxide layer covering the whole surface of the support was obtained. According to the authors of the cited articles, the catalys thus prepared have unique properties. In particular, the catalysts exhibit good selectivity. Thus, the catalysts prepared according to reference [5] are used for selective propane preparation from CO and H2. The catalyst described in reference [6] is used during ethanol dehydrogenation, this catalyst being more active and selective than a catalyst prepared by impregnation or Nb2θ5. The catalyst cited in reference [8] activates the formation of isopentan from methanol. The common feature of the methods cited in references [5] [8] is that first, a thin oxide layer is prepared on the surface of the support. The starting metal compound is chosen such that it does not fit into the cavities of the zeolite [5, 8]. McDaniel has studied the state of chromium(VI) on a Philli polymerisation catalyst [9] and he has also, together with Stricklen, patented a process for preparing a CO-reduced chromyl halide silica-supported catalyst [10]. The startin compounds chosen include Crθ2Cl2. Crθ2 2 and Crθ2 Cl. Befo depositing the starting compound on the support, the surfa of the support was heated in an oxidising ambient, such as air, at a temperature within the range of 400 to 1000 β C in order to remove the hydroxyl groups on the support. After the oxidising treatment, the oxygen was purged by nitrogen or argon gas flushing. At normal pressure and at a temperature ranging from 100 to 400*C, a known amount of t reagent, in the example 0.5 to 4.0 ml of chromyl chloride, was then injected into a stream of nitrogen gas conducted through the support, the reagent vapours reacting with the hydroxyl groups of the support. Unreacted reagent vapour w withdrawn from the reactor. The surfaces of the support particles used in heterogeneou catalysts are structurally inhomogeneous. As far as zeolit are concerned, the chrystalline structure of the material also complex containing, e.g., pore openings having dia¬ meters ranging from 0.3 to 0.7 nm. As a consequence of the above characteristics, the surfaces of the support materia are chemically inhomogeneous containing numerous binding sites of different valencies for new atoms or molecules contacted with the surface of the support. It is difficult to control the binding of the metals or metal compounds us as reagents when following any of the conventional practic described above in references [5] to [10]. The conventional processes also present difficulties in achieving homogeneous dispersion of the metals or the meta compounds on the support surfaces. The present invention aims at eliminating the drawbacks of the prior art and at providing an entirely novel technical solution for gas phase preparation of heterogeneous cata¬ lysts. The invention is based on the concept of bringing the cata lyst reagent in vapour state to the reaction chamber in an amount that at least corresponds to the amount of binding sites on the support surface. It is preferred to use an excess of reagent in relation to the available surface binding sites. The temperature of the support is kept high than the condensation temperature of the vapour and sufficiently high for the active species or its precursor to be chemisorbed on the surface of the support. In other words, the process aims at providing the thermal activatio energy needed for the formation of bonds between the activ species or its precursor and the surface of the support. In particular, the process according to the invention is mainly characterised by what is stated in the characterisi part of claim 1. The apparatus for preparing the heterogeneous catalyst according to the invention is characterised by what is stated in the characterising part of claim 15. Surprisingly, it transpires that under the above-mentioned conditions a heterogeneous catalyst is obtained, whose activity even at small amounts of the active species is high. We do not yet fully understand all the reasons underlying this phenomenon and we do not wish to limit the invention any particular theory. It does, however, appear possible that, under the conditions of the invention, the binding o the active species to the different binding sites of the surface is determined by the structural geometry of the surface atoms of the support and by the electron distribu ion (the surface energy potential). Thus, the chemisorpti of the active species is surface selective. For the purposes of the present application, the followin definitions are used: Catalyst reagent denotes a starting material in solid, liquid or gaseous state, whose vapour contains the compon which together with the support forms the catalytically active sites on the surface of the support. The catalyst reagent employed can comprise any conventional reagent us for the preparation of heterogeneous catalysts, be it in t form of a gas or of a compound that can be volatilised. T reagent may, thus, comprise, inter alia, elemental metals, such as zinc, metal compounds, such as rhenium oxides and chromium halide compounds, and metal complexes, such as Mg(thd) 2 . The active species refers to the catalytically active component on the surface of the support, which can be in the form of an atom, an ion, a molecule, a chemical compou or a complex. Normally, the active species is comprised o the ion, atom or compound of a metal on the surface of th support. The term "precursor" denotes basic forms of the active species which may be inactive but which will yield the active species by a suitable treatment. The support comprises a solid material which has a rather large surface for binding the catalytically active materi or compound. The area of the support surface typically amounts to between 10 and 1000 m 2 /g as determined by the method. The support may consist of an inorganic oxide, su as silica (silica gel), aluminium oxide (alumina), thoriu oxide (thoria), zirconium oxide (zirconia), magnesium oxid (magnesia), or a mixture thereof. These types of supports are essentially catalytically inactive. The support used also comprise a substance which itself catalyses the desir chemical reaction. These supports are exemplified by the natural or synthetic zeolites. It is to be understood that, within the scope of this application, the term "support" also encompasses inactive supports having a catalytically active species bound to their surface. Thus, for instance, when bimetal catalysts are prepared, the first species may provide the support surface for the second species. The reaction chamber is the space, within which the support and the reagents are contacted. Chemisorption refers, in general, to a process, in which the gaseous, liquid or dissolved compound is bound or attached to the surface of a solid or liquid substance in such a way that a bond, essentially of a chemical nature, is formed. Physical adsorption (or physisorption) is a process which, in essence, involves the physical adsorption of a substance on the surface of another substance by intermolecular force known as the van der Waals forces. Condensation means the liquidification or solidification of vapours and gases by cooling. The present process comprises three basic stages, including the pre- and posttreatment stages, which are part of the preferred embodiments of the invention, although they are not essential as far as the basic solution of the invention is concerned. The process parameters of the method are the temperatures and the duration of each of the given stages. The selection of process parameters is influenced by the actual support- reactant combination. In the present invention, all the reagents for the pre- treatment, for the binding of the catalytically active species and for the posttreatment are routed to the reacti chamber in vapour form typically one at the time. The vapo pressure of the vaporized catalyst reagent is maintained a a sufficiently high level and the duration of its interact ion with the surface of the support is sufficiently pro¬ longed that at least an equal amount or, preferably, an excess of the reagent is provided in relation to the binding sites available on the support. In relation to the atom layer or molecular layer filling all of the available surface binding sites, a 1.5- to 1000-fold surplus of the reagent and preferably a 2-to 100-fold surplus is normally used. The monolayer amount of the species can be calculate using, for instance, the BET method on the basis of the surface of the support and the molecular structure of the surface. in the context of the invention, reaction conditions are sought in which the gas-phase reagent (the active species its precursor) fills all or essentially all of the binding sites available to provide saturation of the surface at th prevailing temperature. During the reaction, the temperature should not be allowed to drop below the vaporization temperature of the reagent. Neiter must the reagent be allowed to condense on its rout to the reaction chamber, but the temperature of the feed piping should be kept close to the reaction temperature. The reagent and the temperature employed are selected in such a way that the reagent does not decompose and the decomposition products, if any, do not condense. In a preferred embodiment of the invention, a temperature gradient is formed, increasing from the reagent source towards the reaction chamber. It is possible experimentally to determine a temperature range, or temperature interval, within which the reaction is most advantageously conducted. The lower limit of the temperature range is determined by the condensation temperature of the evaporated reagent and the activation energy necessary for establishing the desired surface bond. The condensation temperature is not, by itself, an appropr ate lower limit if it is too low to provide the reagent wi the energy needed for surpassing the activation threshold. The upper limit is determined by the temperature at which the active species, or its precursor chemisorbed on the support, starts to show a significant rate of desorption from the binding site, i.e. when the equilibrium of the chemisorption-desorption reaction has shifted toward de¬ sorption. The reagent is selected such that the activation energy required by the chemisorption is exceeded at a temperature at which desorption is still not significant. in most cases, the activation and desorption energies are not known and, thus, the selection of suitable reactants an temperatures is determined by experimentation. In the process consituting part of the present invention, the pretreatment, the binding and the posttreatment temperatures of the catalytically active component can differ from each other. However, it is required that limit T m in, for for each reagent used, be exceeded during each process stage. Sometimes the temperature of the pre- treatment will influence the amount of active species or it precursor bound to the support. This is the case, for examp when chromium is bound to the surface of silica. The bindin temperature (>T m i n ) might then, in turn, influence the amount of the active species or its precursor chemisorbed t the support. This phenomenon can be illustrated by the preparation of the alumina-supported rhenium and the silica supported zinc catalysts. As will become evident from the following examples, the temperature is generally kept below 500*C, although this temperature does not represent an absolute upper limit. The reaction between the catalyst reagent vapour and the support may be carried out at elevated pressure, ambient pressure or in a vacuum. In the preferred embodiment of the invention, the process is carried out at a reduced pressure ranging from 0.1 to 100 mbar. The benefit to be gained by using reduced pressure resides in improved purit of the reaction chamber and increased diffusion rate. The pretreatment and posttreatment stages can, similarly, be carried out at elevated pressure, ambient pressure or reduced pressure. The reaction time is predominantly affected by the penetration of the vapour molecules into the pores or cavities of the support. The gas diffusion between the support particles constitutes an extremely fast process in comparison to the diffusion towards the inner parts of the pores. The reaction time should be kept long enough to all the vapour containing the active component to interact wit the binding sites of the support and to provide the desire surface saturation. In the experiments conducted, the results have indicated that the reaction time can be selected in the range from 0.5 to 25 hours. Usually 1 to 4 hours is enough for achieving the desired goal. In practice, the above-mentioned process parameters must b determined experimentally, since it is practically impossi to determine the exact binding properties between the support and the gas molecules. Almost every bound species affects and changes the surface areas immediately adjacent which gives cause to changes in the surface potential. Summarising, the different stages of the process can be characterised as follows: Pretreatment: As mentioned above, the basic structure of the support materials of the heterogeneous catalyst are different. Thu the atoms or molecules of the vapour-phase catalytically active substance may, under the same ambient conditions, react in very different ways with different supports. The pretreatment stage of the support is, therefore, important. The pretreatment aims at providing the desired binding site for the catalytically active component that is to be bound to the support. The pretreatment can be effected by heating the support or by treating it chemically or as a combination of these two operations. The heat treatment can, for instance, comprise increasing the temperature of the support to the same temperature as used for binding the active component. In this case, it is preferable for temperature to be increased at a steady rate over a given period of time. The support may also be heated for some time, normally for between 1 min and 100 hours, preferably from between about and 30 hours, at a selected pretreatment temperature that i either higher, as high as or lower than the temperature use for binding the component. The suitable temperature depends on the support, on the catalytically active species to be bound, and on the binding temperature selected. A pretreat¬ ment temperature higher than the reaction temperature leads with a high probability, to a stable and reproducable surface situation in the actual reaction stage. Too high a pretreatment temperature may, however, change the desired surface structure of the support. At too low a temperature, it is not possible efficiently to remove undesired molecule of substances physically adsorbed on the surface. In the chemical treatment of the support, the support can b treated with a chemical substance, such as water (steam), f forming hydroxyl groups on the surface, or alternatively, with a dehydrating agent for removing hydroxyl groups. The support can also be treated with a volatile metal compound, such as a magnesium or titanium compound. It is also possible to combine the above-mentioned heat treatment and the chemical treatment, the support being heated to or maintained at the desired temperature, while subsequently contacting the surface with a chemical substance, such as steam. Thus, according to one embodime of the invention, the support is pretreated at a high temperature for removing adsorbed water. After this, the temperature of the support may possibly be changed and st allowed to interact with the surface, on which chemisorpt of new hydroxyl molecules can then proceed. The actual reaction is thus finally carried out either at the same o at another temperature. The binding of the active species: The surface-activated support is contacted and interacts with vapour containing the component (i.e. species of pre cursor) that is to be bound. The component is bound to th surface by selectively filling the available surface bind sites. As mentioned above, the temperature and the durati of the process are determined experimentally for each support material, while taking the activation conditions the characteristics of the vapour containing the binding component into account. Several different kinds of active species may be bound to the support as an outcome of the process in the invention. In a multi-species catalyst, the binding order may vary, result being different kinds of catalysts. Modification of the binding surrounding of the catalytica active species: In order to optimise the properties of the catalyst, the prepared specimen can, if necessary, be subjected to post treatment. This may, for instance, comprise a heat treatm in which the catalyst is heated to a desired temperature which generally is at least in excess of the binding temperature. When the degree of oxidation of the active s of the catalyst is to be changed, the heat treatment is carried out in oxidising or reducing conditions. During the heat treatment the catalyst atoms may be contac with a vapour, e.g. steam, that modifies the binding surrounding. This modification may be necessary, e.g. when the precursor of the catalytically active species comprise a reagent molecule deposited on the surface of the support, a part of which is to be removed after the binding. Thus, to continue the example, chlorine atoms are often detrimental to the activity of the catalyst and they can b removed by steam or hydrogen sulfide treatment. in order to modify the properties of the catalyst, a singl or several further species may be added by repeating the procedure described above in such a manner that a vapour containing a new species or its precursor is chosen for th actual binding reaction. The stages of the process can be repeated for a desired amount of new species, with the option to conduct heat treatment and/or chemical treatmen between the stages. There are considerable benefits to be gained by the invention. Thus, for example, in the case of chromium- titanium/silica and rhenium/alumina catalysts, the catalyst have been found to be active at lower metal loadings than previously reported in the literature. This would suggest that the metal is more evenly distributed than in the catalysts prepared from solutions. The ability to control the binding of the metal during the preparation is improved It is easier to bind several metals than from solution. The metal may be bound in the form of different compounds to t same support, with the necessary ligands being readily obtainable. The impurities caused by the reagents are diminished. The temperature of the process may, in some cases, be lowered. As a product of the process described in the invention, heterogeneous catalysts exhibiting different basic structur may be prepared. The catalysts used in oil refining, the metathesis catalysts and the polymerisation catalysts may b mentioned by way of example. In the following discussion, the main groups of catalysts are represented by zeolite- supported zinc, alumina-supported rhenium and silica- supported chromium. However, it is also possible to prepar other noble metal catalysts and transition metal catalysts In the following, the invention will be examined with the aid of a detailed description and working examples. It should be noted that the description relates only to some of the preferred embodiments of the invention. Within the scope of the invention, however, other embodiments are quite as conceivable. Figure 1 shows in cross-section one possible reactor desig for carrying out the process according to the invention. Figures 2 and 3 depict the binding of Zn on the surface of zeolite support as a function of the binding temperature. Figure 4 portrays the influence of support preheating on t binding of chromium from Crθ2Cl2 to silica. Figure 5 depicts the binding of chromium to silica as a function of the reaction temperature. Figure 6 illustrates the activity of a silica-supported chromium catalyst in comparison to a prior art catalyst. Apparatus used for preparing the catalysts according to the invention The test reactor used in the working examples comprises a longish reactor body 1 and a reactor chamber 4 fitted with said reactor body. In the reactor chamber, there is a container 5 for the sample 6, i.e. the support material. I the reactor body 1 at the end containing the reactor chamb 4, there is a loading/unloading cover 3 for exchanging the reactor chamber with the sample container 5. In order to seal the reactor body 1 hermetically, the cover 3 is provi ded with suitable sealings, such as annular sealing rings. Heating elements 7, 8, 9, are mounted around the reactor body 1 for providing the necessary temperature in the different parts of the reactor. The heating elements 7, 8, can, for instance, consist of heat resistances. A protecting gas, typically nitrogen and/or argon, is fed into the reactor chamber 4 through a feed conduit 10, the gas atmosphere within the reactor body 1 being controlled by a regulator mounted on the feed conduit 10. In order to provide reduced pressure, the reactor chamber 4 can be connected to a vacuum pump 24 by means of a suction pipe 25. The vacuum pump is also connected to the gas space defined by the reactor body 1 via a vacuum pipe 11. The vacuum pump used may be of a conventional membrane or pisto pump type. If necessary, a liquid nitrogen trap should be fitted between the pump 24 and the evacuated spaces for collecting condensing fumes. There are two feed conduits 12 and 13 fitted within the reactor chamber 4. It is possible to feed vaporized catalys reagent via these pipes to the reactor chamber 4. The feed pipe 12 is connected to a gas source, the reagent transport gas being fed into the pipe at the point indicated with an arrow. The gas flow is controlled by a regulator 17. The vessel 16, which is also referred to in the following as th hot source, is used for reagents that are solid or liquid a ambient temperature. The reagent is vaporized by heating it to the desired vaporizing temperature by means of heaters 8 and 9. By adjusting the gas flow with the aid of the regulator 17, it is possible to control the flow of the reagent vapour generated in the hot source to the reaction chamber 4. The second feed piping 13 is connected to two gas sources 1 and 15 used for feeding reagents that are vaporous or liqui at ambient temperature. Pressurised reagent is fed from the gas source 14, which typically is a gas cylinder, via a valve 18 to the feed pipe 13. The gas source 15 is used for reagents having a rather low vapour pressure in compariso to the reaction chamber. These reagents are normally liqu at room temperature. The regulators, i.e. for instance th valves 19, 20, 21, control the flow of the reagents from gas source 15 to the feed pipe 13. The feed pipe 13 is connected before the regulator 21 to the transport gas source at the point indicated by an arrow (pipe section 26 The transport gases used for feeding the reagents from gas sources 14 and 15 preferably comprise inert gases, such as nitrogen and/or argon. The reagents used for the chemical pretreatment are fed fr sources 14, 15 or 16, respectively. The apparatus used in the working examples further include a mass spectrometer 22 for analysing volatile reaction products from samples withdrawn through the regulator 27. The mass spectrometer also comprises a two-part pump arrangement 23 including a prepump and a high pressure pu The apparatus is used as follows: A suitable amount of a support material 6 is placed in the sample container 5 in the reaction chamber 4. In the worki examples, the scale of the operation has been small, and usually samples weighing in a range from 3 to 10 g have b used. A liquid or solid reagent is placed in container 16. The reactor body 1 and the reaction chamber 4 are subsequently evacuated by feeding protecting gas via the feed conduit 10 and the feeding pipe 13 at a low flow rate (controlled by regulator means 28 and 21), while providin reduced pressure in the reaction chamber 5 by means of vacuum source 24. Normally, the goal is to achieve a pressure amounting to a few millibars, e.g. 3 to 10 mbar. If necessary, the support 6 is then pretreated. As mention above, the heat treatment may be carried out using various heating times and temperatures; the temperature is normall in the range from about 200 to about 500 β C, whilst the heating time is about 10 to 30 hours. During this period o time the reagent in container 16 is not normally heated. During chemical pretreatment or blocking, the reactants ar fed from sources 14, 15 or 16. Thus, e.g. steam is conduct from source 15 by routing the protecting/transport gas flo via source 15 (valve 21 is closed and valves 20 and 19) ar opened. Before initiating the reaction, the temperature of the reagent in source 15 is increased to the desired level by the heater 9. Use of the heater 8 enables an increasing temperature gradient to be established between the hot source 16 and the reactor chamber 4, the temperature of the reactor chamber 4 being higher that the temperature of the hot source 16. The regulator 17 is next opened and reactant vapour is fed by the transport gas into the reactor chamber 4. The reactant is metered at a dosage larger than that required by the number of surface binding sites. The gaseous reagent diffuses into the support 6 in the samp container 5 and the surplus gas is withdrawn through channe 25 by means of the vacuum pump 24. A part of the gas stream flowing from the reaction chamber 4 is conducted via valve 27 to the mass spectrometer for analysis of its composition When using gaseous reagents, these are fed from gas sources 14 and 15. The reagents that are gaseous at room temperatur are preferably fed from a gas cylinder 14, and liquid reagents from a liquid container 15. The reagents flowing through the feed pipe 13 are heated to the desired temperature by heaters 8 and 9. The temperature of the feed pipe is always kept higher than the condensation temperatur of the reagents. The process is continued until the desired surface reaction has reached a state of saturation. The supply of the reagen is then cut off. The temperature and the pressure are returned to normal (STP). If necessary, the catalyst is removed from the apparatus in an atmosphere of protecting gas. Preparation of the catalysts: 1. Supports and reagents The zeolite support was comprised of a mixture of a HZSM-5 type zeolite and silica. The zeolite was prepared as follows: 2300 g of tetra-propy ammonium bromide, 100 g of sodium aluminate, 2760 g of sil gel (Ludox), 114 g of sodium hydroxide and 18500 g of wate were transferred into an autoclave, the temperature was increased to 165 β C, and the chemicals were allowed to reac for 144 h. The mixture was then rapidly cooled to ambient temperature, after which the product was recovered and was with 150 1 water. The product obtained was dried for 24 h 120 β C and calcined for 15 h at 540 β C. The sodium-containin zeolite was ion exchanged with a 5 % w/w ammonium nitrate solution. The ion exchanged product was dried for 24 h at 120'C. Next, the zeolite was calcined for 15 h at 540 # C. When the HZSM-5 zeolite (Si/Al = 40) was ready, 100 g of t zeolite, 100 ml of silica gel (Ludox AS-40) and 10 ml of water were mixed in a mortar, moulded into cakes, dried fo 12 h at 115 β C, powdered and calcined for 2 h at 540 β C. The support materials, silica and the y-aluminium oxide we of commercial quality. The most important data on the support materials are given Table 1: Table 1. The properties of the support materials The following reagents were used: metallic zinc, zinc chloride (ZnCl2). chromium chloride (Crθ2Cl2). rhenium heptoxide (Rβ2θ7), aluminium chloride (AICI3), titanium chloride (TiCl4) and magnesium dipivaloyl-methane [Mg(thd)2]« The materials were of commercial grade, except for the last one, which was synthesized as described in the publication Hammon, G.S. et al., Inorg Chem 2 (1963), p 73. The surface of the metallic zinc was treated with hydro chloric acid in order to remove the surface layer before use. Otherwise, the reagents were not pretreated. 2. Analysis The amounts of elements bound to the supports were determin by means of atomic absorption spectrometry (Al, Ti, Cr, Zn) fluorescence spectroscopy (Zn), polarimetric titration (Cl) or neutron activation analysis (Re). X-ray induced photo- electron spectroscopy (XPS or ESCA) and X-ray diffraction analysis (XRD) were employed for evaluation of the metals on the surface of the catalyst. Example l : The preparation of a zinc/zeolite catalyst This example illustrates the binding of a metal in elemen state to the surface of the support. Further, the impact the reaction temperature on the amount of metal bound to surface is considered in the example. The zinc/zeolite catalyst is used in oil refining, e.g., catalysing the conversion of butane to aromatic compounds Several catalysts were prepared by binding zinc to the surface of zeolites. The support material lot weighing 2 to 10 g was placed in a sample vessel of a reaction cha where it was heat treated at 430 to 465"C in a nitrogen stream of 2 to 5 mbar pressure. The pretreatment time was 2 to 24 h. Metallic zinc placed in a heated source was heated to 430 and the zinc vapour was routed to the reaction chamber. During each test the temperature of the reaction chamber maintained above 430 β C in order to prevent the condensati of zinc onto the zeolite surface. The zinc vapour was reacted with the zeolite for 1 to 4 h. The Zn concentrations in the preapared catalysts were bet 0.03 and 10 % w/w. Some of the catalysts thus obtained were subsequently treated with sulphur. Elemental sulphur was placed in the hot source and sulphurous fumes evaporated from it were reacted with the Zn/zeolite catalyst at 465 # C. The binding of Zn as a function of the reaction temperatu is depicted in Figure 2. The Figure shows only the result obtained after 2 hours 1 preheating. Extension of the pre¬ heating period to 24 hours did not increase the binding o zinc to any larger extent. The logarithm of the ratio of atoms to Siθ2+Al2θ3 atoms was calculated for Figure 2. Th Zn concentration of the catalyst was measured giving the amount of Zn atoms per zeolite weight unit. From the known BET surface of the zeolite the number of surface molecules was calculated. As a reference, the number of Zn atoms or ZnO molecules in an atom or molecule layer completely covering the surface (monolayer, ML) was calculated. The binding of the zinc is influenced by the adsorption, the formation of a chemical bond and the desorption. Figur 2 shows that decreasing temperature and vapour pressure of zinc will reduce the amount of zinc bound to the surface. According to the present invention, the minimum temperatur is represented by the condensation temperature of zinc, 390°C. The binding of zinc is also substantially decreased when the temperature rises above 500°C, which possibly is caused by the fact that the desorption of zinc is faster than at binding temperatures below 500°C. The maximum temperature of the process in accordance with the inventio is, in this case, about 500 β C. Example 2 The preparation of a zinc/zeolite catalyst If the vapour pressure of a metal is low (e.g. less than 0. mbar) within the temperature range used for the preparatio of a catalyst, more volatile inorganic metal compounds or organo metal compounds can be employed. Thus, zinc/zeolite catalysts were also prepared starting from zinc chloride. The binding temperature was in the ran from 355 β C to 455 β C. A steam treatment was effected in ord to reduce the amount of the chloride ion residue on the catalyst. Instead of steam, hydrogen sulphide may, for instance, be used as well. In the above manner catalysts were provided having zinc contents in the order of 1 % w/w. Figure 3 depicts the binding of zinc from ZnCl2 to zeolite as a function of the reaction temperature. Example 3 The activity of the zinc/zeolite catalysts The activity of the zeolite-supported zinc catalysts was evaluated by testing the catalysts for the conversion of n-butane into aromates and for aromate selectivity. The t were carried out in a microreactor at ambient pressure and at temperatures ranging from 450 to 500 # C. The quantity o the catalyst batch loaded in the reactor was 5.0 g and the feed rate of n-butane into the reactor was 5 g/h. The reaction was monitored with the help of gas chromatography a sample being taken after each five hours 1 run at 450*C constant temperature. out of the zeolite-supported zinc catalysts prepared accor ding to the invention, three catalyst were subjected to analysis runs. Two of the catalysts had been prepared at 430 β C and the third one at 470 β C. The catalysts contained 0.66, 0.65 and 1.07 % w/w, respectively, of zinc. The supp of the first catalyst had been pretreated for 2 hours at 500 β C before the binding reaction. Reference catalysts wer prepared by the dry impregnation technique, which involved impregnating 0.5 ml zinc nitrate solution into each g of an H-ZSM5-zeolite/silica support. Said catalysts were drie at 115 β C for 12 h, and subsequently calcined at 540*C for 4 hours. The catalysts prepared by impregnation contained 0.15 and 1.4 % w/w, respectively, of zinc. The test results are shown in Table 2: Table 2. Butane conversion and aromate yield As is evident from the results, the catalysts produced in accordance with the invention achieve an equal or higher degree of conversion than is obtained with the reference catalyst, while the selectivity to aromatic compounds is at least at an equal level. Both the conversion and the aromat selectivity are on an industrially applicable level. Example 4 The preparation of a Re/Al2θ3 catalyst The Re/alumina combination is a well-known metathesis catalyst which can be used, e.g., for catalysing the dispro portionation of propene to ethene and butene. Following to the process outlined for the invention, rhenium was bound to the surface of y-alumina from rhenium heptoxide, which i a solid substance at ambient temperature. The catalysts were prepared using coarse-grain alumina as support. Rβ2θ7 (Aldrich Chemicals Co., purity: 99.9 %) was volatilized by heating it at 160 β C. The preheating of the support and the binding of the rhenium were carried out a 3 mbar nitrogen pressure. The reaction temperature was mai tained in the range from 175 to 360 β C, an increasing temperature gradient being formed from the hot source towards the reaction chamber. The rhenium heptoxide vapour was contacted with the support for 225 minutes. The rheni content of the prepared catalyst was determined. Table 3 gives the pretreatment and reaction temperatures. Table 3. Re/y-Al2θ3 catalysts The table indicates that a long pretreatment at high temperatures decreases the amount of rhenium binding to th support. The largest amounts of rhenium are bound to the surface of alumina without any heat pretreatment. Test were further carried out to study the influence of a Mg(thd)2 addition on the support's capability to sorb rhe¬ nium. The alumina was first heated at 475 β C for 18 hours, then cooled to 240 β C and, subsequently, contacted with fum of Mg(thd)2 that had been volatilized at a temperature ranging from 75 β C to 85 β C. In this case, 0.36 % rhenium was bound to the support from rhenium heptoxide. In a reference test, in which no magnesium dipivaloylmethane wa used, the rhenium content was 0.12 %. Thus, the amount of Re bound to the support was tripled by the Mg(thd)2 treatment. The amount of Re bound to the support was rather small in all the tests (< 0.65 %) in comparison to conventional Re metathesis catalysts that can have a Re content of up to 15 %. The activity of the prepared catalysts were assessed on basis of propene conversion. The results indicated that the Re activities on a weight basis were at least as high as those of conventional catalysts, andin several cases muc higher. Thus, in the case of the catalyst 4.2, the propene conversion per weight unit of Re was as high as over 6 % an in the case of catalyst 4.8 even exceeded 15 %. Example 5 The preparation of a chromium/silica catalyst Silica-supported chromium is a known Phillips-type polymeri sation catalyst. The following example will show in more detail, how the preheating and the reaction temperatures influence the binding of chromium in the process according to the invention. Chromyl chloride, Crθ2C_-2 was used as a starting coumpound for the chromium. A silica support (Crosfield Catalysts EP 10 silica gel) the amount of which was 4 to 5.5 g, was pre¬ heated at 100 β C to 360 β C in a nitrogen gas atmosphere at a pressure of 3 to 4 mbar for 17 to 20 hours. After the pre¬ heating the temperature was adjusted to the actual process temperature. Chromyl chloride was evaporated and reacted with the silica at 175, 270 and 365'C temperatures. The reaction time was in excess of 1.5 hours, typically 2.5 hours. Table 4 gives the test operating conditions of three Cr catalyst tests: Table 4. Operating conditions of Cr catalyst tests The Crθ3 layer completely covered the surface of the sili support and was calculated to contain about 0.16 g chromi per 1 g silica. This corresponds to a molar content of approx. 0.003 mol chromium. The reagent used in the tests exceeded the aviable binding sites on the support by abou 30- to 70-fold. The preheating temperature determines the number of OH- groups in silica and thus the number of binding sites. Th chromyl chloride molecule can bind either to one or two hydroxyl groups releasing one or two molecules of HC1, respectively. The highest chromium concentrations were fo after preheating at 270 β C. Reaction temperatures for chro chloride between 150 and 330 # C did not have a major effec on the chromium concentration. The average Cr concentration as a function of the pretrea ment temperature is shown in Figure 5. Figure 6 shows the influence of the reaction temperature the binding of chromium. In a similar manner as in Figure the ratio between the catalytically active metal and the support molecules was calculated. The figure also include an indication of the respective amounts of chromium and chromium oxide covering the silica surface in the form of a monolayer. When the preheating temperature is raised ab 480*C, the Cr concentrations were less than 0.02 %, irrespective of whether the reaction temperatures were 175, 270 or 360 β C. It is worth noting that, according to reference [10], the pretreatment should generally be conducted at a temperatur of at least 400 β C, preferably at a temperature in the rang from 600 to 800 β C. Example 6 Chromium-titanium/silica and chromium-aluminium/silica catalysts In this example, the binding of a second catalytically active metal on the catalyst prepared in Example 5 was studied in detail. Table 5 contains a summary of the operating conditions of these tests: Table 5. The test run conditions of Cr-Ti and Cr-Al catalys In test 6.1, following the preheating step, the support was treated with steam for 75 min at 360 β C, after which the chromyl chloride was added. When the reaction was completed a new water vapour (steam) treatment was conducted at 270 C C followed by the introduction of 0.13 mol of titanium chloride (TiCl4) per unit weight (g) of the support into th same reaction space at the same temperature for 184 minutes Finally, a further steam treatment was performed for 75 minutes. In test 6.2, following the pretreatmen , the support was acted with titanium chloride (5 mmol per g of support) at 270*C for 8.3 min. A water vapour treatment was the perfo for 15 minutes at the same temperature prior to the introduction of chromyl chloride into the reaction chambe In test 6.3, a Cr-containing silica catalyst was prepared described in Example 5 above. The product thus prepared w reacted with titanium chloride at 270*C for 8.3 min. The amount of titanium chloride used corresponded to 9.5 mmol Ti/g of support. In test 6.4, following the pretreatment, the support was first reacted with aluminium chloride (AICI3) at 270 β C fo 150 minutes. The amount of aluminium corresponded to 2.4 mmol Al per unit weight (g) of the support. Steam was the introduced into the reactor chamber for 75 minutes. The chromyl chloride was added as explained in Example 5. The catalysts prepared contained 0.016 to 0.47 % w/w chromium, 0.32 to 6.2 % w/w titanium and 0.49 % w/w aluminium. Example 7 The catalyst activity of Cr/silica-based catalysts The catalysts prepared according to Examples 5 and 6 were fluidized in dry air and heated first to 200 to 250 β at which temperature they were held for 4 h, after which they were finally activated by calcination at an elevated temperature (580 to 780 β C) for about 5 h. The calcined material was cooled to 300 β C and the air atmosphere was replaced by an oxygen-free nitrogen atmosphere. The catalysts thus treated were used in the polymerizatio of ethene. The reaction temperature was 105 β C and the tot pressure 4000 kPa. The hydrocarbon diluent in the polymer ization process was isobutane. The results are shown in Table 5, below. Table 5. Activities of Cr and Ti containing catalysts in polymerization of ethene. As is evident from the results, the catalysts have a very high activity even in those cases where the metal content is low. The catalyst activity of the catalysts prepared according the invention have also been compared with the catalyst di closed in reference [10]. The results are given in Figure In Figure 6, the X-axis indicates the percentage of chromi in the catalysts, and the Y-axis gives the amount of polyethylene formed per weight of the catalyst on an hourl basis. The lines drawn at an angle of 45" to the X-axis indicate the amount of polyethylene formed per hour in relation to the weight of the chromium on the catalyst. The McDaniel and Stricklen catalysts contain about 1 % Cr. Figure 6 shows that, calculated on the basis of PE-convers per unit catalyst weight, the present Cr catalyst attains almost as high an activity at lower Cr loadings as the bes prior art catalysts. At the same time, it should be noted that the known catalysts have been subjected to a separate reducing treatment. From a calculation of the catalyst activity on the basis of the amount of chromium, it appear that the catalysts prepared according to the invention ar considerably more active that the prior art catalysts. Th addition of titanium increases the activity of Cr+Ti cata lysts. Since the catalysts is retained in the product aft the reaction, a decrease in the amount of Cr will provide a valuable additional benefit for catalysts prepared according to the invention.

Claims: < -u Claims : 1. A process for preparing a heterogeneous catalyst having at least one catalytically active species bound to the surface of a support material, said process comprising the steps of - optionally pretreating the surface of the support, - vaporizing a catalyst reagent containing the catalytically active species or its precursor, - routing the vapour into a reaction chamber where it is brought to interact with the support material, th support being kept at a higher temperature than the condensation temperature of the vapour, - removing the catalyst reagent not bound to the support, and subsequently - if necessary, posttreating the species bound to the support in order to convert it into a catalytically active form, c h a r a c t e r i z e d by - maintaining the vapour pressure of the vaporized catalyst reagent in the reaction chamber at a sufficiently high level and the duration of inter¬ action with the support over a sufficiently long period as to provide at least an equal amount of catalyst reagent in relation to the number of avail¬ able binding sites on the support, and - maintaining the temperature of the support at a sufficiently high level to attain chemisorption of the catalytically active species or its precursor to the binding sites of the support. 2. The process as claimed in claim 1, c h a r a c t ¬ e r i z e d by providing an excess of the catalytic reage in relation to the available binding sites of the support. 3. The process as claimed in claim 1, c h a r a c t e r - i z e d by continuing the interaction between the support and the catalytic reagent until at least an essential par of the surface binding sites has been occupied. 4. The process as claimed in any one of claims 1 to 3, c h a r a c t e r i z e d by maintaining the temperature below the temperature at which the catalytically active species begins essentially to desorb from the support. 5. The process as claimed in any one of claims 1 to 4, c h a r a c t e r i z e d by evaporating the catalyst reagent in a separate space and by forming an increasing temperature gradient between said space and the reaction chamber. 6. The process as claimed in any one of claims 1 to 5, c h a r a c t e r i z e d by subjecting the support to a pretreatment by heat. 7. The process as claimed in claim 6, c h a r a c t e r i z e d by subjecting the support to pretreament not onl by heat but also by chemical processing, e.g. with steam a dehydrating agent. 8. The process as claimed in claim 6, c h a r a c t e r i z e d by carrying out the pretreatment of the support the actual reaction in the same reaction chamber. 9. The process as claimed in claim 1, c h a r a c t e r i z e d by carrying out the actual reaction at reduced pressure, typically at a pressure in the range of 0.1 to 100 mbar. 10. The process as claimed in claim 1, c h a r a c t e r i z e d by modifying the oxidation state of the catalyti ally active site by heat treatment in oxidising or reduci conditions. 11. The process as claimed in claim 1, c h a r a c t e r i z e d by posttreating the combination consisting of th catalytically active species and the support by contactin said combination with a vapour that modifies the binding surrounding of the catalyst atoms. 12. The process as claimed in claim 11, c h a r a c t e r i z e d by using water steam as said vapour. 13. The process as claimed in any of the preceeding claims, c h a r a c t e r i z e d by repeating the process steps at least once for at least one additional catalytically active compound. 14. The process as claimed in any of the preceeding claims, c h a r a c t e r i z e d by maintaining the temperature during each process step higher than the condensation temperature of each catalytically active compound used. 15. Apparatus for preparing a heterogeneous catalyst comprising at least one catalytically active compound and a support, said apparatus comprising - a reactor body (l), - a gas tight reaction chamber (4) fitted within the reactor body (1) for holding the support material (6) - heaters (7, 8, 9) placed around the reactor body (1) for achieving the desired temperature in the reactor body (1) and in the reaction chamber (4), - feed (12, 13) and outlet (25) piping connected to the reaction chamber (4) for achieving a protective gas atmosphere inside the reaction chamber, - gaseous reagent sources(14, 15, 16) connected to the reaction chamber (4) for feeding the catalyticall active compound to the reaction chamber space ( ) , an - means for withdrawing unreacted gaseous reagent sur¬ plus, c h a r a c t e r i z e d in that - the gas sources (14, 15, 16) are connected to the inert gas feed piping (12, 13) and - the feed piping (12, 13) is at least partially placed within the reactor body (1) such that the material flowing in the pipes can be heated to the desired reaction temperature by the heatars (7, 8, 9) . 16. The apparatus as claimed in claim 15, c h a r a c t e r i z e d in that the heaters (7, 8, 9) are adjusted to form an increasing temperature gradient in the directi of reagent feed. 17. The apparatus as claimed in claim 15, c h a r a c t - e r i z e d in that the means for withdrawing the unreac reagent comprises the outlet pipe (25) of the inert gas. 18. The apparatus as claimed in claim 15, c h a r a c t ¬ e r i z e d in that at least one gas source comprises an open vessel (16) fitted within a feed pipe (12) in which a starting compound in the solid state can be placed and fr which the starting compound can be vaporized by means of heater (9) . ig. The apparatus as claimed in claim 15, c h a r a c t ¬ e r i z e d in that at least one gas source comprises a liquid starting compound source (14). 20. The apparatus as claimed in claim 15, c h a r a c t - e r i z e d in that at least one gas source comprises a gaseous starting compound source (15).

Inventors: KNUUTTILA HILKKA, KNUUTTILA PEKKA, KRAUSE OUTI, LAKOMAA EEVA-LIISA, SUNTOLA TUOMO, KNUUTTILA, HILKKA, KNUUTTILA, PEKKA, KRAUSE, OUTI, LAKOMAA, EEVA-LIISA, SUNTOLA, TUOMO
Applicants: NESTE OY
Application year: 1991
Main classification: B01J37
IPC codes: B01J23, B01J29, B01J37, C08F4, C08F10