Title of Invention	PROCESS FOR THE PREPARATION OF A KETONE OR AN ALDEHYDE USING SILICA AS A CATALYST
Abstract	The invention relates to a process for the preparation of a ketone and/or an aldehyde, comprising the steps of: a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase, b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising siiica, said silica having a purity higher than 95 wt.%, whereby the ketone and/or the aldehyde is/are formed and whereby the reaction conditions are such that the conversion of at least the understoichiometrically present starting compound(s) is at least 50%.

Title of Invention

PROCESS FOR THE PREPARATION OF A KETONE OR AN ALDEHYDE USING SILICA AS A CATALYST

Abstract

The invention relates to a process for the preparation of a ketone and/or an aldehyde, comprising the steps of: a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase, b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising siiica, said silica having a purity higher than 95 wt.%, whereby the ketone and/or the aldehyde is/are formed and whereby the reaction conditions are such that the conversion of at least the understoichiometrically present starting compound(s) is at least 50%.

Full Text	PROCESS FOR THE PREPARATION OF A KETONE QR AK ALDEHYDE USING SILICA AS A CATALYST The invention relates to a process for the preparation of a ketone and/or an aldehyde; in particular, the invention relates to a process for the preparation of an unsaturated ketone and/or an unsaturated aldehyde from a starting ketone or a starting aldehyde or a mixture of a starting ketone and a starting aldehyde. Such a process is generally known as an aidol condensation. An example thereof is disclosed in the Journal of Catalysis 106, pages 273-279 (1987), wherein the production of methyl vinyl ketone from formaldehyde and acetone is disclosed. The known process is a vapour-phase aldol condensation between formaldehyde and acetone using various kinds of single and binary metal oxides and heteropoly compounds as catalysts. The known process preferably uses V2O5-P2O5 (P/V atomic ratio - 1.06) and Fe203-P2O5 (P/Fe - 4.6) catalysts. The known process has as disadvantage that the yield is still unsatisfactory; a yield (based on formaldehyde) of about 40% at a contact time of 10 seconds is reported, and a yield of up to about 65% at extended contact times is reported. It is the objective of the present invention to reduce the said disadvantage. The objective is achieved in a process for the preparation of a ketone and/or an aldehyde, comprising the steps of: a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase; b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising silica, said silica having a purity higher than 95 wt.Vo, whereby the ketone and/or the aldehyde is/are formed and whereby the reaction conditions are such that the conversion of the stoichiometrically least present starting compound(s) is at least 50%. The advantage of the present invention is that higher yields can be achieved than in the known process. US-A-3,928,458 discloses that alpha, beta-unsaturated aldehydes, ketones, nitriles and esters are formed by the vapor phase condensation of saturated aldehydes, ketones, nitriles and alkyl esters of aliphatic monocarboxylic acids with formaldehyde in the presence of an unmodified silica gel catalyst, with reported conversions of formaldehyde of up to 45%. In step a) of the process according to the invention, a reaction mixture is formed. The reaction mixture should comprise, as starting compound or starting compounds, a starting ketone or a starting aldehyde or a mixture of a starting ketone and a starting aldehyde. Moreover, the reaction mixture should be in the gaseous phase. As starting ketone, in principle any known ketone or mixture of ketones is suitable, provided that the ketone of mixture of ketones is in the gaseous phase or can be brought in the gaseous phase. Ketones as such are known; preferably, a C3 - C10 aliphatic, cyclic or aromatic ketone is used. Preferred examples of ketones suitable as starting ketone include acetone, methylethylketone (MEK) and mesityloxide (4-methylpent-3-en-2-one). Within the context of the present invention, a reference to a (starting) ketone embraces the reference to a mixture of different (starting) ketones; in a preferred embodiment of the invention, the starting ketone is a mixture of ketones. As starting aldehyde, in principle any known aldehyde or mixture of aldehydes is suitable, provided that the aldehyde or mixture of aldehydes is in the gaseous phase or can be brought in the gaseous phase. Aldehydes as such are known; preferably, aC1- C1o aliphatic, cyclic or aromatic aldehyde is used as starting aldehyde. Preferred examples of suitable starting aldehydes include formaldehyde and acetaidehyde. Within the context of the present invention, a reference to a (starting) aldehyde embraces the reference to a mixture of different (starting) aldehydes; in a preferred embodiment of the invention, the starting aldehyde is a mixture of aldehydes. The reaction mixture may be formed by taking a desired amount of starting material or materials and - in case there is more than one starting material - combining them, while preferably performing a mixing operation; if the starting material(s) is/are not in the gaseous phase, then they should be brought in the gaseous phase through means that are as such known to the skilled person, e.g. through a heating step or a decomposition step. An example of such a decomposition step is the decomposition of paraformaldehyde or trioxan to form formaldehyde. If the starting material(s) is/are already in the gaseous phase, then step a) of the present invention can already be executed through the mere taking or combining and preferably mixing of the starting material(s). The starting material may be present as such (e.g. in pure form), or it may be present in the form of a mixture with another compound, e.g. as an aqueous solution which is quite common in for example formaldehyde. In case the reaction mixture comprises various compounds, then it may be desirable to introduce a mixing step so as to homogenise the reaction mixture prior to the execution of step b). The reaction mixture may comprise additional compounds besides the starting ketone, the starting aldehyde, and water. Examples of such additional compounds are stabilizing compounds, such as methanol in case formaldehyde is used, or inert gases such as for example nitrogen, carbon dioxide, or argon. In a preferred embodiment of the invention, however, the amount of such additional compounds is limited to about 50 wt.%, 40 wt.%, 25 wt.% or even 20 or 10 or 5 wt,% of the reaction mixture, Most preferably, the reaction mixture contains essentially no additional compounds except stabilizing compounds; this has the advantage that these compounds do not need to be removed from the reaction mixture afterwards in order to isolate valuable compounds such as the ketone and/or the aldehyde. Within the context of the present invention, the terms 'contain essentially no' or 'consist essentially of or equivalents are understood to mean that if there are any further compounds present or if other measures are taken, then these further compounds or measures have no significant influence on the functioning of the invention or on the effects as achieved by the invention. Subsequent to the forming of the reaction mixture in step a) according to the invention, step b) is executed. In step b), the gaseous reaction mixture is brought in contact with a catalyst. Typically, and preferably, the catalyst will be a solid. The bringing in contact of the reaction mixture with the catalyst may be done by means known as such; a typical example of such a known means is putting the catalyst in a reactor and forcing the gaseous reaction mixture to flow through the reactor. The catalyst in the process according to the invention comprises silica, i.e. oxide of silicon. Silica as such is widely known. It was found, surprisingly, that the yield of the process according to the invention can be higher than in the known process if the silica as comprised in the catalyst has a high purity of at least 95, 96, 97,98 or 99 wt.%. Preferably, the purity of the silica is at least 99.1, 99.2 or 99.3 wt.%; more preferably, the purity of the silica is al least 99.4, 99.5,99.6, 99.7 or even 99.8 wt.%;. Without committing to scientific explanation, it is thought that whereas in many other cases silica merely acts as and is used as a support for catalyst particles, the silica itself is - surprisingly - in the process according to the invention the catalyst. It is therefore additionally preferred that the catalyst as used in the process according to the invention comprises at least 50 or 60 wt.% of high-purity silica; more preferably, the catalyst as used in the process according to the invention comprises at least 75, 85 or even 90 or 95 wt.% of high-purity silica; most preferably, the catalyst as used in the process according to the invention consists essentially or even only of high'purity silica. It is preferred that if there are any compounds comprised in the catalyst besides silica, then these are essentially devoid of Al2O3 , ZrO2, P2O5, V2O5, Ce2O3, TiO2, and NB2O; it was found that the said compounds are among the compounds that can have a negative influence on the yield and/or selectivity of the ketone- or aldehyde-forming reaction. In a preferred embodiment according to the invention, the silica as comprised in the solid catalyst comprises or even consists essentially of fumed silica. As is known, a fumed silica preferably consists of clusters of primary non-porous particles, whereby the cluster structure creates pores. This structure results in the fumed silica having a high specific surface area; preferably, this specific surface area lies between 25 and 500 m /g, more preferably between 50 and 450 m2/g. It is furthermore preferred that the fumed silica has an amount of at most 20% micropores or even at most 15% or 10% or essentially no micropores at all. Preferably, thus, the catalyst is essentially free of micropores. Micropores are defined as pores having a diameter of 5 ran or less. The low amount or even absence of micropores is advantageous as micropores are difficult to access for the compounds in the reaction mixture, or even not accessible at all. It is furthermore preferred that the low amount of micropores is combined with an average pore size lying between 5 and 100 run, more preferably between 6 nm and 50 nrn. Most preferably, the amount of pores having a diameter of more than 100 nm is at most 10%, 5% or even at most 1%; as a consequence of this, the pore size distribution will be relatively narrow. The low amount or even absence of micropores can contribute to the catalyst having a specific surface area that lies lower than values of 500 or even 600 mVg. Preferably, therefore, the specific surface area of the catalyst as used in the process of the invention is at most 400, 350, 300 or even at most 250 or 200 m2/g. This has - in particular in combination with a low amount or even absence of micropores - the advantage that maximum use can be made of essentially the whole of the specific surface area of the catalyst, thus contributing to a high degree of-con version. In order to contribute to a high degree of conversion even in a limited reaction space, it is preferred that the silica catalyst has a specific surface area of at least 25, 50, 75 or 100m2/g. As is known, fumed silica - also referred to as pyrogenic silica - is different from silica gel. Whereas silica gel is typically prepared by the neutralization of aqueous alkali metal silicate with acid, fumed silica is typically prepared by vaporizing a silicon tetrahalide such as silicon tetrachloride, mixing it with dry air and hydrogen, then feeding the mixture to a burner and hydrolyzmg it. The differences between silica gel and fumed silica are further elucidated in literature, such as in the Silica chapter of Ullmann's Encyclopedia of Industrial (Electronic version) as posted online on 15.09.2000 with DOI 10.1002/14356007.a23 583. In a preferred embodiment of the invention, the catalyst does not consist essentially of silica gel. It is moreoover preferred that the catalyst as used in the process according to the invention contains at most 75%, 50% or 40 wt.% of silica gel. More preferably, the catalyst as used in the process according to the invention contains at most 30, 20 or 10 wt.% of silica gel. Most preferably, the catalyst as used in the process according to the invention is essentially free of silica gel. Once the reaction mixture has been brought in contact with the catalyst, the catalytic activity will lead to the formation of the - typically unsaturated - ketone and/or the -typically unsaturated - aldehyde. It is preferred hereby, and in many cases even necessary, that step b) is carried out at an elevated temperature lying preferably between 250°C and 500°C. More preferably, the temperature at which step b) is carried out is at least 275, 300, or even 320 or 325°C; the temperature at which step b) is carried out is preferably at most 475, 450, or 425°C; more preferably at most 400, 390,380, or 375°C. It will typically not be very beneficial to carry out the process according to the invention at significantly elevated or reduced pressure, although this is possible in a very wide range between 0.005 MPaand 15 MPa. The contact of the reaction mixture with the catalyst can lead to several types of reaction mechanisms, which are embraced within the context of the present invention. The reactions may take place on the surface of the catalyst or they may take place in the gaseous phase, e.g. by a reactive intermediate compound that was formed on the catalyst and then detached from it. The reactions taking place at the catalyst may start either from a ketone, from an aldehyde, or from both. The nature of the starting ketone and /or the starting aldehyde will co-determine which ketone or mixture of ketones and/or which aldehyde or mixture of aldehydes will be formed. As is the case in the known process, the presence of acetone as the starting ketone and formaldehyde as the starting aldehyde can lead to the formation of a.o. methylvinylketone (MVK), a know compound having formula (I): (Formula Removed) Since MVK is a compound having commercial importance, a.o. as intermediate compound in the synthesis of Vitamin A, astaxanthin and zeaxanthin, the reaction mixture in a preferred embodiment of the process according to the invention comprises upon its formation both a starting ketone and a starting aldehyde, whereby acetone is primarily or even essentially only the starting ketone and formaldehyde is primarily or even essentially only the starting aldehyde. It was found that a high selectivity towards formation of MVK can be reached in case of a molar excess of acetone over formaldehyde; preferably, therefore, the molar ratio between acetone and formaldehyde is at least 9:1; more preferably, the said ratio is at least 12:1 or 15:1; most preferably, the molar ratio between acetone and formaldehyde in the reaction mixture is at least 18:1 or even 20:1. For practical reasons, the molar ratio between acetone and formaldehyde is at most 100:1. The molar ratios as given here are applicable to the reaction mixture as it is formed, and/or at the onset of step b) as the reaction mixture comes in contact with the catalyst. As indicated above, the formation of a reaction mixture comprising formaldehyde may for practical reasons involve the use of an aqueous solution of formaldehyde; such solutions, e.g. comprising 37 wt.% formaldehyde in water, are known. Generally speaking, the person skilled in the art would expect that the presence of water has a negative influence on the overall yield of the reaction since water is a by-product of MVK formation and thus could lead to an equilibrium shift away from MVK formation. It was surprisingly found, however, that the presence of water in the reaction mixture in step a) or at the onset of step b) does not have a negative effect; by contrast, a positive effect on the yield of MVK was observed. In a preferred embodiment of the invention, therefore, the weight ratio of formaldehyde to water in the reaction mixture is in step a) or at the onset of step b) at most 60:40, 50:50 or 40:60, preferably at most 30:70 or 25:75, most preferably at most 20:80. The reaction mixture as a whole preferably comprises - at the onset of the execution of step b)-at least 1 wt.% of water, more preferably at least 5, 10 or even 15 wt.%; the reaction mixture as a whole preferably comprises - at the onset of the execution of step b) -at most 50 wt.% water, more preferably at most 40, 30 or 20 wt.%. The steps a) and b) according to the invention may be carried out in batch operation or in continuous operation. In any case, it is preferred that the residence time of the reaction mixture in step b), in particular the contact time between catalyst and reaction mixture, is chosen such that an adequate reaction progression is combined with an economical mode of operation. In achieving this, it is helpful to consider the residence time parameter W/F; this widely used parameter is defined as the amount of catalyst present (in grams) divided by the flow of the reaction mixture (in total amount of moles of all compounds in the reaction mixture per hour), In the process according to the invention, it is preferred that W/F lies between 1 and 1000 g.h/mol, more preferably between 10 and 750 g.h/mol, in particular between 20 and 500 g.h/mol, and most preferably between 40 and 150 g.h/mol. The process according to the invention should be carried out such that a main objective, being a high conversion of the starting compound(s), can be achieved in step b). It is hereby noted that if there are several starting compounds in the reaction mixture and if there is a molar excess of one of the starting compounds, then the term conversion as meant herein should be evaluated on that starting compound or that mixture of starting compounds that is understoichiometrically present. A non-limiting example of such a situation is when the reaction mixture contains acetone and formaldehyde as starting compounds, whereby the acetone is present in excess and the formaldehyde is the understoichiometrically present starting compound. The process according to the invention should be carried out in such a way that the conversion in step b) of at least the understoichiometrically present starting compound(s) is at least 50%. Preferably, the process according to the invention is carried out such that the conversion in step b) of at least the understoichiometrically present starting compound(s) is at least 60%, 70% or even at least 80%. The said conversions may be achieved by selecting the high purity catalyst according to the invention in combination with favourable combinations of reaction conditions in step b), optionally combined with an excess of a starting compound. It was found that important reaction conditions in this respect are the temperature and the residence parameter W/F; furthermore, it was found that the structure of the catalyst can be beneficial in this regard. As described above, the temperature in step b) preferably lies between 250°C and 500°C. More preferably, the temperature at which step b) is carried out is at least 275, 300 or even 320 or 325°C; the temperature at which step b) is carried out is preferably at most 475, 450 or 425°C; more preferably at most 400, 390, 380 or 375DC. Also, as described above, it is preferred that W/F lies between I and 1000 g.h/mol, more preferably between 10 and 750 g.h/mol, in particular between 20 and 500 g.h/mol, and most preferably between 40 and 150 g.h/mol. A specific choice of the composition or structure of the silica catalyst can further contribute to achieving an enhanced conversion, e.g by selecting a very high purity and/or by selecting turned silica and/or by ensuring that the fumed silica has a low amount of micropores. The person skilled in the art will be able to find through routine optimisations within the ranges as given the conditions that enable him to achieve a conversion of at least 50% preferably at least 60, 70 or 80%. The said routine optimisations will also yield those combinations of catalyst type and reaction conditions that combine a high conversion of the starting compound(s) with a high selectivity towards the desired ketone and/or aldehyde to be formed. As described earlier, a high selectivity may be further enhanced by other measures such as the presence of water in the reaction mixture. If the reaction mixture comprises acetone as the starting ketone and formaldehyde as the starting aldehyde, and if there is a molar excess of acetone, then the situation can arise that the reaction mixture comprises a high amount of acetone as starting ketone subsequent to the execution of step b). It is then - and also in other embodiments of the invention involving an excess of one of the reactants and/or an incomplete conversion - typically desirable to recover the starting ketone and/or the starting aldehyde from the reaction mixture. The invention therefore further also relates to a process comprising after step b) the steps of: c) feeding the reaction mixture to a rectification apparatus; d) separating a top stream comprising the starting ketone and/or the starting aldehyde from the reaction mixture and removing it from the rectification apparatus; e) optionally recycling at least a portion of the top stream to step a) or step b). In step c) according to the invention, the reaction mixture is fed to a rectification apparatus. Rectification apparatuses are as such known; an example of such an apparatus is a distillation column. It is preferred to feed the reaction mixture to the rectification apparatus with the reaction mixture being in the gaseous phase, preferably without having undergone phase changes subsequent to the completion of step b). This has, in combination with the subsequent steps d) and e), the advantage that hardly any energy related to changing of phase is lost in the recovery of the starting ketone and/or the starting aldehyde. In the rectification apparatus, step d) according to the invention takes place: a -preferably gaseous - stream comprising the starting ketone and/or the starting aldehyde is separated from the reaction mixture, and subsequently removed from the rectification apparatus. Since this stream will often be removed from the upper half of the apparatus, it is hereby named the top stream. The forming of the top stream by separating it from the reaction mixture may be achieved by means known as such to the skilled person, such as distillation techniques. Also the removal of the top stream from the rectification apparatus may be achieved by means known as such to the skilled person, such as pumping or pressure reduction. The top stream may now, after having been removed from the rectification apparatus, be advantageously re-used in the process according to the invention. The invention therefore preferably comprises - subsequent to step d) - a step e), in which at least a portion of the top stream is recycled to step a) or step b). The said portion is preferably at least 25 wt.% of the top stream, more preferably at least 50 wt.% or even at least 75 wt.%. The separating off of a portion from the top stream and the subsequent recycling may be achieved by means as such known to the skilled person. It may be additionally advantageous to separate a second portion off from the top stream, condense this second portion and feed it back to the rectification apparatus as a reflux stream. As is know to the skilled person, such reflux streams are often beneficial or even necessary in achieving a satisfactory composition of the top stream and in achieving a satisfactory energy efficiency of operation of the rectification apparatus. The starting ketone and/or starting aldehyde as comprised in the .top stream can - as described above - be beneficially recycled to step a) or b) of the process according to the invention so as to aid in forming the reaction mixture. Depending on the nature of the top stream, it may be necessary to implement one or more purification steps on the top stream so as to remove any unwanted compounds. With the top stream separated off from the reaction mixture, the reaction mixture may be removed from the rectification apparatus as well - preferably after the reaction mixture has been brought into liquid form. Depending on the circumstances, subsequent steps may be desirable in order to isolate the ketone and/or the aldehyde from the reaction mixture. Examples of such steps are rectification, filtration, extraction, crystallisation, and the like. In case the reaction mixture comprises acetone as starting ketone and formaldehyde as starting aldehyde, then - as indicated above - MVK can be prepared. When a gaseous reaction mixture comprising MVK is then according to step c) fed to a rectification apparatus and brought into liquid form, it was found that it is important to ensure that undesirable subsequent reactions of MVK such as polymerisation are minimised. It is therefore a further object of the invention to provide a method for reducing or even preventing the said subsequent reactions of MVK. The said method comprises the step of mixing an MVK-stabilizing agent with MVK when the MVK is transferred from the gaseous phase into the liquid phase or immediately thereafter. The MVK-stabilizing agent preferably comprises water; more preferably, the MVK-stabilizing agent comprises a mixture of water with an acid. Preferably, the acid is acetic acid. In particular, the MVK-stabilizing agent comprises besides water and an acid such as acetic acid also hydroquinone. If the MVK-stabilizing agent comprises hydroquinone, then it is preferred that it also comprises acetonitrile. In a preferred embodiment of the invention, the MVK-stabilizing agent has the following composition: - between 30 and 95 wt.% acetic acid, preferably between 50 and 90 wt.%; - between 1 and 40 wt.% water, preferable between 10 and 30 wt.%; -betweenOand 15 wt.% hydroquinone, preferably between 0.1 and 10wt.%; - between 0 and 15 wt.% acetonitrile, preferably between 0.1 and 10 wt.%, whereby the sum of these four compounds adds to 100%. The amount of MVK-stabilizing agent as added to the reaction mixture, or to the MVK itself after having been further purified, may vary between wide limits and lies preferably between 0.1 and 10 wt.% relative to the amount of MVK. The minimisation of undesirable subsequent reactions of ketones such as MVK or of aldehydes may also be supported by choosing favourable process conditions. It was found that the speed of said undesirable subsequent reactions is reduced with reducing temperature; this may be achieved by for example carrying out the process in the rectification apparatus at reduced pressure. Furthermore, it was found that the absence of light also contributes to the control of undesirable subsequent reactions. MVK is, as indicated above, a compound having various known uses, a.o. as intermediate in processes for the preparation of vitamin A, astaxanthin or zeaxanthin. The invention therefore also relates to processes for the preparation of vitamin A or astaxanthin or zeaxanthin, comprising the process for MVK preparation according to the invention. The preparation of MVK constitutes one example of the industrial applicability of the process according to the invention. Other examples of unsaturated ketones that may be formed according to the invention are: the preparation of mesityloxide from a reaction mixture comprising acetone as starting ketone and no starting aldehyde; and the preparation of 3-methylcyclohexenon from a reaction mixture comprising formaldehyde as starting aldehyde and mesityloxide as starting ketone. The compound 3-methylcyclohexenon is as such known and has formula (II): (Formula Removed) Examples of unsaturated aldehydes that may be prepared according to the invention are: acrolein (CH2 = CH-CHO), which may be prepared from a reaction mixture containing CH3-CHO and CH20 as starting aldehydes; and crotonaldehyde (CH3-CH=CH-CHO), which may be prepared from reaction mixture containing CH3-CHO as starting aldehyde. Generally speaking, it will be advantageous to choose the starting material(s) such that the formation of those ketones and/or aldehydes is targeted that permit handling in the gaseous phase at the prevailing temperatures in step b). A quick or even immediate phase transfer of the ketones and/or aldehydes as formed into the liquid or solid phase would be more likely to cause processing problems and is thus less preferred. The invention will be illustrated by means of the following examples, without being limited thereto. Examples 1-5 and Comparative Experiment A The preparation of MVK according to steps a) and b) was executed in a unit comprising a vaporiser and a reactor. The vaporiser comprised twp sections: in the first section acetone was vaporised by means of heating; in the second isection a 37 wt.% aqueous formaldehyde solution was vaporised by means of spraying it into the gaseous acetone stream and heating; hereby the reaction mixture was formed. "The heating was done such that the reaction mixture had a temperature of 350°C. The reaction mixture was then fed to a reactor containing a catalyst. The temperature in the reactor was also kept at 350°C. The catalyst type is as given in the table below. As the reaction mixture exited the reactor, a sample was taken and analysed. Each sample was taken after the catalyst had been in operation for 10 hours except in examples 4 and 5 where the catalyst had been in operation for 30 hours. (Table Removed) Notes to the table: Aeroiyst 3045 is a fumed S1O2 catalyst of 99% purity, supplied by Degussa; the BET surface area was determined at 155 m2/g. Pural MG 70 is a hydrotalcile (MgO / A1203) supplied by Condea, having a BET surface area of 23 m2/g. Aeolyst 350 is a fumed SiO2 catalyst of 99% purity. SA3235 is a AI2O3-S1O2 catalyst supplied by Norton®.The residence time parameter W/F of the reaction mixture in the reactor is expressed as g.h/mol, as is usual for the skilled person. The yield of MVK as given is based on the amount of formaldehyde in the feed to the reactor. From the table, it is clear that the Aerolyst catalysts according to the invention has a much higher yield than the about 65% as reported in the Journal cjf Catalysis, and also has a higher yield than the 50% as found for the hydrotalcite catalyst. [Also, it is clear that a catalyst comprising not only Si02 but also AI2O3 - SA3235 - sho^s a high yield, albeit somewhat less than when a catalyst comprising only high-purity SJi02 is used. Furthermore, it is clear that an increase in the ratio of acetone to formaldehyde jeads to an increase of the selectivity towards MVK formation. Claims 1. Process for the preparation of a ketone and/or an aldehyde, comprising the steps of: a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase; b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising silica, said silica having a purity higher than 95 wt.%, whereby the ketone and/or the aldehyde is/are formed and whereby the reaction conditions are such that the conversion of at least the understoichiometrically present starting compound(s) is at least 50%. 2. Process according to claim 1, wherein the catalyst consists essentially of fumed silica having a purity higher than 98 wt.% and having a specific surface area lying between 25 and 500 m2/g, 3. Process according to claim 1 or 2, wherein the catalyst is essentially free of micropores. 4. Process according to any one of claims 1 - 3, wherein the starting ketone comprises acetone, the starting aldehyde comprises formaldehyde, and wherein in step a) the molar ratio between acetone and formaldehyde in the reaction;mixture lies between 9:1 and 100:1. 5. Process according to claim 1, wherein the reaction mixture comprises, at least at the moment it is brought in contact with the catalyst, between 1 and 50 wt.% water. 6. Process according to any one of claims 1 - 5, wherein the reaction mixture comprises, at least at the moment it is brought in contact with the catalyst, less than 10 wt.% of compounds other than compounds from the group consisting of aldehydes, ketones, stabilizers, and water. 7. Process according to any one of claims 1 - 6, wherein step b) is carried out ai a temperature lying between 250°C and 400º0. 8 Process according to claim 1, further comprising after step b) the steps of: c) feeding the reaction mixture in the gaseout. phase to a rectification apparatus; d) separating a top stream comprising the starting ketone and/or the starting aldehyde from the reaction mixture and removing it from the rectification apparatus; e) recycling at least a portion of the lop stream to step a) or step b) 9. Process according to claim 8, wherein the starting ketone comprises acetone. 10. Process according to claim 9, wherein in step a» the reaction mixture comprises acetone and formaldehyde in a molar ratic lying between 9:1 and 100:1, wherein the ketone comprises methylvinylketone (MVK), said MVK being transferred into the liquid phase, whereby an MYK-stabilizing compound is mixed with MVK at the moment MVK is liquefied or shortly thereafter. 11. Process according to claim 10, wherein the MVK-stabilizing compound is a mixture comprising at least one of water, acetic acid, hydrochinone and acetonitrile. 12. Process for the preparation of vitamin A., comprising the process according to any one of claims 4 -11. 13. Process for the preparation of astaxanthin, comprising the process according to any one of claims 4 -11. 14. Process for the preparation of zeaxanthin, comprising the process according to any one of claims 4 -11.

Full Text

PROCESS FOR THE PREPARATION OF A KETONE QR AK ALDEHYDE USING SILICA AS A CATALYST
The invention relates to a process for the preparation of a ketone and/or an aldehyde; in particular, the invention relates to a process for the preparation of an unsaturated ketone and/or an unsaturated aldehyde from a starting ketone or a starting aldehyde or a mixture of a starting ketone and a starting aldehyde.
Such a process is generally known as an aidol condensation. An example thereof is disclosed in the Journal of Catalysis 106, pages 273-279 (1987), wherein the production of methyl vinyl ketone from formaldehyde and acetone is disclosed. The known process is a vapour-phase aldol condensation between formaldehyde and acetone using various kinds of single and binary metal oxides and heteropoly compounds as catalysts. The known process preferably uses V2O5-P2O5 (P/V atomic ratio - 1.06) and Fe203-P2O5 (P/Fe - 4.6) catalysts.
The known process has as disadvantage that the yield is still unsatisfactory; a yield (based on formaldehyde) of about 40% at a contact time of 10 seconds is reported, and a yield of up to about 65% at extended contact times is reported.
It is the objective of the present invention to reduce the said disadvantage.
The objective is achieved in a process for the preparation of a ketone and/or an aldehyde, comprising the steps of:
a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase;
b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising silica, said silica having a purity higher than 95 wt.Vo, whereby the ketone and/or the aldehyde
is/are formed and whereby the reaction conditions are such that the conversion of the stoichiometrically least present starting compound(s) is at least 50%.
The advantage of the present invention is that higher yields can be achieved than in the known process.
US-A-3,928,458 discloses that alpha, beta-unsaturated aldehydes, ketones, nitriles and esters are formed by the vapor phase condensation of saturated aldehydes, ketones, nitriles and alkyl esters of aliphatic monocarboxylic acids with formaldehyde in the presence of an unmodified silica gel catalyst, with reported conversions of formaldehyde of up to 45%.
In step a) of the process according to the invention, a reaction mixture is formed. The reaction mixture should comprise, as starting compound or starting compounds, a starting ketone or a starting aldehyde or a mixture of a starting ketone and a starting aldehyde. Moreover, the reaction mixture should be in the gaseous phase.
As starting ketone, in principle any known ketone or mixture of ketones is suitable, provided that the ketone of mixture of ketones is in the gaseous phase or can be brought in the gaseous phase. Ketones as such are known; preferably, a C3 - C10 aliphatic, cyclic or aromatic ketone is used. Preferred examples of ketones suitable as starting ketone include acetone, methylethylketone (MEK) and mesityloxide (4-methylpent-3-en-2-one). Within the context of the present invention, a reference to a (starting) ketone embraces the reference to a mixture of different (starting) ketones; in a preferred embodiment of the invention, the starting ketone is a mixture of ketones.
As starting aldehyde, in principle any known aldehyde or mixture of aldehydes is suitable, provided that the aldehyde or mixture of aldehydes is in the gaseous phase or can be brought in the gaseous phase. Aldehydes as such are known; preferably, aC1- C1o aliphatic, cyclic or aromatic aldehyde is used as starting aldehyde. Preferred examples of suitable starting aldehydes include formaldehyde and acetaidehyde. Within the context of the present invention, a reference to a (starting) aldehyde embraces the reference to a mixture of different (starting) aldehydes; in a preferred embodiment of the invention, the starting aldehyde is a mixture of aldehydes.
The reaction mixture may be formed by taking a desired amount of starting material or materials and - in case there is more than one starting material - combining them, while
preferably performing a mixing operation; if the starting material(s) is/are not in the gaseous phase, then they should be brought in the gaseous phase through means that are as such known to the skilled person, e.g. through a heating step or a decomposition step. An example of such a decomposition step is the decomposition of paraformaldehyde or trioxan to form formaldehyde. If the starting material(s) is/are already in the gaseous phase, then step a) of the present invention can already be executed through the mere taking or combining and preferably mixing of the starting material(s). The starting material may be present as such (e.g. in pure form), or it may be present in the form of a mixture with another compound, e.g. as an aqueous solution which is quite common in for example formaldehyde. In case the reaction mixture comprises various compounds, then it may be desirable to introduce a mixing step so as to homogenise the reaction mixture prior to the execution of step b).
The reaction mixture may comprise additional compounds besides the starting ketone, the starting aldehyde, and water. Examples of such additional compounds are stabilizing compounds, such as methanol in case formaldehyde is used, or inert gases such as for example nitrogen, carbon dioxide, or argon. In a preferred embodiment of the invention, however, the amount of such additional compounds is limited to about 50 wt.%, 40 wt.%, 25 wt.% or even 20 or 10 or 5 wt,% of the reaction mixture, Most preferably, the reaction mixture contains essentially no additional compounds except stabilizing compounds; this has the advantage that these compounds do not need to be removed from the reaction mixture afterwards in order to isolate valuable compounds such as the ketone and/or the aldehyde. Within the context of the present invention, the terms 'contain essentially no' or 'consist essentially of or equivalents are understood to mean that if there are any further compounds present or if other measures are taken, then these further compounds or measures have no significant influence on the functioning of the invention or on the effects as achieved by the invention.
Subsequent to the forming of the reaction mixture in step a) according to the invention, step b) is executed. In step b), the gaseous reaction mixture is brought in contact with a catalyst. Typically, and preferably, the catalyst will be a solid. The bringing in contact of the reaction mixture with the catalyst may be done by means known as such; a typical example of such a known means is putting the catalyst in a reactor and forcing the gaseous reaction mixture to flow through the reactor.
The catalyst in the process according to the invention comprises silica, i.e. oxide of silicon. Silica as such is widely known. It was found, surprisingly, that the yield of the process according to the invention can be higher than in the known process if the silica as
comprised in the catalyst has a high purity of at least 95, 96, 97,98 or 99 wt.%. Preferably, the purity of the silica is at least 99.1, 99.2 or 99.3 wt.%; more preferably, the purity of the silica is al least 99.4, 99.5,99.6, 99.7 or even 99.8 wt.%;. Without committing to scientific explanation, it is thought that whereas in many other cases silica merely acts as and is used as a support for catalyst particles, the silica itself is - surprisingly - in the process according to the invention the catalyst. It is therefore additionally preferred that the catalyst as used in the process according to the invention comprises at least 50 or 60 wt.% of high-purity silica; more preferably, the catalyst as used in the process according to the invention comprises at least 75, 85 or even 90 or 95 wt.% of high-purity silica; most preferably, the catalyst as used in the process according to the invention consists essentially or even only of high'purity silica.
It is preferred that if there are any compounds comprised in the catalyst besides silica, then these are essentially devoid of Al2O3 , ZrO2, P2O5, V2O5, Ce2O3, TiO2, and NB2O; it was found that the said compounds are among the compounds that can have a negative influence on the yield and/or selectivity of the ketone- or aldehyde-forming reaction.
In a preferred embodiment according to the invention, the silica as comprised in the solid catalyst comprises or even consists essentially of fumed silica. As is known, a fumed silica preferably consists of clusters of primary non-porous particles, whereby the cluster structure creates pores. This structure results in the fumed silica having a high specific surface area; preferably, this specific surface area lies between 25 and 500 m /g, more preferably between 50 and 450 m2/g. It is furthermore preferred that the fumed silica has an amount of at most 20% micropores or even at most 15% or 10% or essentially no micropores at all. Preferably, thus, the catalyst is essentially free of micropores. Micropores are defined as pores having a diameter of 5 ran or less. The low amount or even absence of micropores is advantageous as micropores are difficult to access for the compounds in the reaction mixture, or even not accessible at all. It is furthermore preferred that the low amount of micropores is combined with an average pore size lying between 5 and 100 run, more preferably between 6 nm and 50 nrn. Most preferably, the amount of pores having a diameter of more than 100 nm is at most 10%, 5% or even at most 1%; as a consequence of this, the pore size distribution will be relatively narrow. The low amount or even absence of micropores can contribute to the catalyst having a specific surface area that lies lower than values of 500 or even 600 mVg. Preferably, therefore, the specific surface area of the catalyst as used in the process of the invention is at most 400, 350, 300 or even at most 250 or 200 m2/g. This has - in particular in combination with a low amount or even absence of micropores - the advantage that maximum use can be made of essentially the whole of the specific surface area of the catalyst, thus contributing to a high
degree of-con version. In order to contribute to a high degree of conversion even in a limited reaction space, it is preferred that the silica catalyst has a specific surface area of at least 25, 50, 75 or 100m2/g.
As is known, fumed silica - also referred to as pyrogenic silica - is different from silica gel. Whereas silica gel is typically prepared by the neutralization of aqueous alkali metal silicate with acid, fumed silica is typically prepared by vaporizing a silicon tetrahalide such as silicon tetrachloride, mixing it with dry air and hydrogen, then feeding the mixture to a burner and hydrolyzmg it. The differences between silica gel and fumed silica are further elucidated in literature, such as in the Silica chapter of Ullmann's Encyclopedia of Industrial (Electronic version) as posted online on 15.09.2000 with DOI 10.1002/14356007.a23 583. In a preferred embodiment of the invention, the catalyst does not consist essentially of silica gel. It is moreoover preferred that the catalyst as used in the process according to the invention contains at most 75%, 50% or 40 wt.% of silica gel. More preferably, the catalyst as used in the process according to the invention contains at most 30, 20 or 10 wt.% of silica gel. Most preferably, the catalyst as used in the process according to the invention is essentially free of silica gel.
Once the reaction mixture has been brought in contact with the catalyst, the catalytic activity will lead to the formation of the - typically unsaturated - ketone and/or the -typically unsaturated - aldehyde. It is preferred hereby, and in many cases even necessary, that step b) is carried out at an elevated temperature lying preferably between 250°C and 500°C. More preferably, the temperature at which step b) is carried out is at least 275, 300, or even 320 or 325°C; the temperature at which step b) is carried out is preferably at most 475, 450, or 425°C; more preferably at most 400, 390,380, or 375°C. It will typically not be very beneficial to carry out the process according to the invention at significantly elevated or reduced pressure, although this is possible in a very wide range between 0.005 MPaand 15 MPa.
The contact of the reaction mixture with the catalyst can lead to several types of reaction mechanisms, which are embraced within the context of the present invention. The reactions may take place on the surface of the catalyst or they may take place in the gaseous phase, e.g. by a reactive intermediate compound that was formed on the catalyst and then detached from it. The reactions taking place at the catalyst may start either from a ketone, from an aldehyde, or from both.

The nature of the starting ketone and /or the starting aldehyde will co-determine which ketone or mixture of ketones and/or which aldehyde or mixture of aldehydes will be formed. As is the case in the known process, the presence of acetone as the starting ketone and formaldehyde as the starting aldehyde can lead to the formation of a.o. methylvinylketone (MVK), a know compound having formula (I):
(Formula Removed)
Since MVK is a compound having commercial importance, a.o. as intermediate compound in the synthesis of Vitamin A, astaxanthin and zeaxanthin, the reaction mixture in a preferred embodiment of the process according to the invention comprises upon its formation both a starting ketone and a starting aldehyde, whereby acetone is primarily or even essentially only the starting ketone and formaldehyde is primarily or even essentially only the starting aldehyde. It was found that a high selectivity towards formation of MVK can be reached in case of a molar excess of acetone over formaldehyde; preferably, therefore, the molar ratio between acetone and formaldehyde is at least 9:1; more preferably, the said ratio is at least 12:1 or 15:1; most preferably, the molar ratio between acetone and formaldehyde in the reaction mixture is at least 18:1 or even 20:1. For practical reasons, the molar ratio between acetone and formaldehyde is at most 100:1. The molar ratios as given here are applicable to the reaction mixture as it is formed, and/or at the onset of step b) as the reaction mixture comes in contact with the catalyst.
As indicated above, the formation of a reaction mixture comprising formaldehyde may for practical reasons involve the use of an aqueous solution of formaldehyde; such solutions, e.g. comprising 37 wt.% formaldehyde in water, are known. Generally speaking, the person skilled in the art would expect that the presence of water has a negative influence on the overall yield of the reaction since water is a by-product of MVK formation and thus could lead to an equilibrium shift away from MVK formation. It was surprisingly found, however, that the presence of water in the reaction mixture in step a) or at the onset of step b) does not have a negative effect; by contrast, a positive effect on the yield of MVK was observed. In a preferred embodiment of the invention, therefore, the weight ratio of formaldehyde to water in the reaction mixture is in step a) or at the onset of step b) at most 60:40, 50:50 or 40:60, preferably at most 30:70 or 25:75, most preferably at most 20:80. The reaction mixture as a whole preferably comprises - at the onset of the execution of step b)-at least 1 wt.% of water, more preferably at least 5, 10 or even 15 wt.%; the
reaction mixture as a whole preferably comprises - at the onset of the execution of step b) -at most 50 wt.% water, more preferably at most 40, 30 or 20 wt.%.
The steps a) and b) according to the invention may be carried out in batch operation or in continuous operation. In any case, it is preferred that the residence time of the reaction mixture in step b), in particular the contact time between catalyst and reaction mixture, is chosen such that an adequate reaction progression is combined with an economical mode of operation. In achieving this, it is helpful to consider the residence time parameter W/F; this widely used parameter is defined as the amount of catalyst present (in grams) divided by the flow of the reaction mixture (in total amount of moles of all compounds in the reaction mixture per hour), In the process according to the invention, it is preferred that W/F lies between 1 and 1000 g.h/mol, more preferably between 10 and 750 g.h/mol, in particular between 20 and 500 g.h/mol, and most preferably between 40 and 150 g.h/mol.
The process according to the invention should be carried out such that a main objective, being a high conversion of the starting compound(s), can be achieved in step b). It is hereby noted that if there are several starting compounds in the reaction mixture and if there is a molar excess of one of the starting compounds, then the term conversion as meant herein should be evaluated on that starting compound or that mixture of starting compounds that is understoichiometrically present. A non-limiting example of such a situation is when the reaction mixture contains acetone and formaldehyde as starting compounds, whereby the acetone is present in excess and the formaldehyde is the understoichiometrically present starting compound. The process according to the invention should be carried out in such a way that the conversion in step b) of at least the understoichiometrically present starting compound(s) is at least 50%. Preferably, the process according to the invention is carried out such that the conversion in step b) of at least the understoichiometrically present starting compound(s) is at least 60%, 70% or even at least 80%. The said conversions may be achieved by selecting the high purity catalyst according to the invention in combination with favourable combinations of reaction conditions in step b), optionally combined with an excess of a starting compound. It was found that important reaction conditions in this respect are the temperature and the residence parameter W/F; furthermore, it was found that the structure of the catalyst can be beneficial in this regard. As described above, the temperature in step b) preferably lies between 250°C and 500°C. More preferably, the temperature at which step b) is carried out is at least 275, 300 or even 320 or 325°C; the temperature at which step b) is carried out is preferably at most 475, 450 or 425°C; more preferably at most 400, 390, 380 or 375DC. Also, as described above, it is preferred that W/F lies between I and 1000 g.h/mol, more
preferably between 10 and 750 g.h/mol, in particular between 20 and 500 g.h/mol, and most preferably between 40 and 150 g.h/mol. A specific choice of the composition or structure of the silica catalyst can further contribute to achieving an enhanced conversion, e.g by selecting a very high purity and/or by selecting turned silica and/or by ensuring that the fumed silica has a low amount of micropores. The person skilled in the art will be able to find through routine optimisations within the ranges as given the conditions that enable him to achieve a conversion of at least 50% preferably at least 60, 70 or 80%. The said routine optimisations will also yield those combinations of catalyst type and reaction conditions that combine a high conversion of the starting compound(s) with a high selectivity towards the desired ketone and/or aldehyde to be formed. As described earlier, a high selectivity may be further enhanced by other measures such as the presence of water in the reaction mixture.
If the reaction mixture comprises acetone as the starting ketone and formaldehyde as the starting aldehyde, and if there is a molar excess of acetone, then the situation can arise that the reaction mixture comprises a high amount of acetone as starting ketone subsequent to the execution of step b). It is then - and also in other embodiments of the invention involving an excess of one of the reactants and/or an incomplete conversion - typically desirable to recover the starting ketone and/or the starting aldehyde from the reaction mixture. The invention therefore further also relates to a process comprising after step b) the steps of:
c) feeding the reaction mixture to a rectification apparatus;
d) separating a top stream comprising the starting ketone and/or the starting aldehyde from the reaction mixture and removing it from the rectification apparatus;
e) optionally recycling at least a portion of the top stream to step a) or step b).
In step c) according to the invention, the reaction mixture is fed to a rectification apparatus. Rectification apparatuses are as such known; an example of such an apparatus is a distillation column. It is preferred to feed the reaction mixture to the rectification apparatus with the reaction mixture being in the gaseous phase, preferably without having undergone phase changes subsequent to the completion of step b). This has, in combination with the subsequent steps d) and e), the advantage that hardly any energy related to changing of phase is lost in the recovery of the starting ketone and/or the starting aldehyde.
In the rectification apparatus, step d) according to the invention takes place: a -preferably gaseous - stream comprising the starting ketone and/or the starting aldehyde is separated from the reaction mixture, and subsequently removed from the rectification apparatus. Since this stream will often be removed from the upper half of the apparatus, it is hereby named the top stream. The forming of the top stream by separating it from the reaction mixture may be achieved by means known as such to the skilled person, such as distillation techniques. Also the removal of the top stream from the rectification apparatus may be achieved by means known as such to the skilled person, such as pumping or pressure reduction.
The top stream may now, after having been removed from the rectification apparatus, be advantageously re-used in the process according to the invention. The invention therefore preferably comprises - subsequent to step d) - a step e), in which at least a portion of the top stream is recycled to step a) or step b). The said portion is preferably at least 25 wt.% of the top stream, more preferably at least 50 wt.% or even at least 75 wt.%. The separating off of a portion from the top stream and the subsequent recycling may be achieved by means as such known to the skilled person.
It may be additionally advantageous to separate a second portion off from the top stream, condense this second portion and feed it back to the rectification apparatus as a reflux stream. As is know to the skilled person, such reflux streams are often beneficial or even necessary in achieving a satisfactory composition of the top stream and in achieving a satisfactory energy efficiency of operation of the rectification apparatus.
The starting ketone and/or starting aldehyde as comprised in the .top stream can - as described above - be beneficially recycled to step a) or b) of the process according to the invention so as to aid in forming the reaction mixture. Depending on the nature of the top stream, it may be necessary to implement one or more purification steps on the top stream so as to remove any unwanted compounds.
With the top stream separated off from the reaction mixture, the reaction mixture may be removed from the rectification apparatus as well - preferably after the reaction mixture has been brought into liquid form. Depending on the circumstances, subsequent steps may be desirable in order to isolate the ketone and/or the aldehyde from the reaction mixture. Examples of such steps are rectification, filtration, extraction, crystallisation, and the like.
In case the reaction mixture comprises acetone as starting ketone and formaldehyde as starting aldehyde, then - as indicated above - MVK can be prepared. When a gaseous
reaction mixture comprising MVK is then according to step c) fed to a rectification apparatus and brought into liquid form, it was found that it is important to ensure that undesirable subsequent reactions of MVK such as polymerisation are minimised. It is therefore a further object of the invention to provide a method for reducing or even preventing the said subsequent reactions of MVK. The said method comprises the step of mixing an MVK-stabilizing agent with MVK when the MVK is transferred from the gaseous phase into the liquid phase or immediately thereafter. The MVK-stabilizing agent preferably comprises water; more preferably, the MVK-stabilizing agent comprises a mixture of water with an acid. Preferably, the acid is acetic acid. In particular, the MVK-stabilizing agent comprises besides water and an acid such as acetic acid also hydroquinone. If the MVK-stabilizing agent comprises hydroquinone, then it is preferred that it also comprises acetonitrile. In a preferred embodiment of the invention, the MVK-stabilizing agent has the following composition:
- between 30 and 95 wt.% acetic acid, preferably between 50 and 90 wt.%;
- between 1 and 40 wt.% water, preferable between 10 and 30 wt.%; -betweenOand 15 wt.% hydroquinone, preferably between 0.1 and 10wt.%;
- between 0 and 15 wt.% acetonitrile, preferably between 0.1 and 10 wt.%,
whereby the sum of these four compounds adds to 100%.
The amount of MVK-stabilizing agent as added to the reaction mixture, or to the MVK itself after having been further purified, may vary between wide limits and lies preferably between 0.1 and 10 wt.% relative to the amount of MVK.
The minimisation of undesirable subsequent reactions of ketones such as MVK or of aldehydes may also be supported by choosing favourable process conditions. It was found that the speed of said undesirable subsequent reactions is reduced with reducing temperature; this may be achieved by for example carrying out the process in the rectification apparatus at reduced pressure. Furthermore, it was found that the absence of light also contributes to the control of undesirable subsequent reactions.
MVK is, as indicated above, a compound having various known uses, a.o. as intermediate in processes for the preparation of vitamin A, astaxanthin or zeaxanthin. The invention therefore also relates to processes for the preparation of vitamin A or astaxanthin or zeaxanthin, comprising the process for MVK preparation according to the invention.
The preparation of MVK constitutes one example of the industrial applicability of the process according to the invention. Other examples of unsaturated ketones that may be formed according to the invention are: the preparation of mesityloxide from a reaction mixture comprising acetone as starting ketone and no starting aldehyde; and the preparation of 3-methylcyclohexenon from a reaction mixture comprising formaldehyde as starting aldehyde and mesityloxide as starting ketone. The compound 3-methylcyclohexenon is as such known and has formula (II):
(Formula Removed)
Examples of unsaturated aldehydes that may be prepared according to the invention are: acrolein (CH2 = CH-CHO), which may be prepared from a reaction mixture containing CH3-CHO and CH20 as starting aldehydes; and crotonaldehyde (CH3-CH=CH-CHO), which may be prepared from reaction mixture containing CH3-CHO as starting aldehyde.
Generally speaking, it will be advantageous to choose the starting material(s) such that the formation of those ketones and/or aldehydes is targeted that permit handling in the gaseous phase at the prevailing temperatures in step b). A quick or even immediate phase transfer of the ketones and/or aldehydes as formed into the liquid or solid phase would be more likely to cause processing problems and is thus less preferred.
The invention will be illustrated by means of the following examples, without being limited thereto.
Examples 1-5 and Comparative Experiment A
The preparation of MVK according to steps a) and b) was executed in a unit comprising a vaporiser and a reactor. The vaporiser comprised twp sections: in the first section acetone was vaporised by means of heating; in the second isection a 37 wt.% aqueous formaldehyde solution was vaporised by means of spraying it into the gaseous
acetone stream and heating; hereby the reaction mixture was formed. "The heating was done such that the reaction mixture had a temperature of 350°C. The reaction mixture was then fed to a reactor containing a catalyst. The temperature in the reactor was also kept at 350°C. The catalyst type is as given in the table below. As the reaction mixture exited the reactor, a sample was taken and analysed. Each sample was taken after the catalyst had been in operation for 10 hours except in examples 4 and 5 where the catalyst had been in operation for 30 hours.

(Table Removed)
Notes to the table: Aeroiyst 3045 is a fumed S1O2 catalyst of 99% purity, supplied by Degussa; the BET surface area was determined at 155 m2/g. Pural MG 70 is a hydrotalcile (MgO / A1203) supplied by Condea, having a BET surface area of 23 m2/g. Aeolyst 350 is a fumed SiO2 catalyst of 99% purity. SA3235 is a AI2O3-S1O2 catalyst supplied by Norton®.The residence time parameter W/F of the reaction mixture in the reactor is expressed as g.h/mol, as is usual for the skilled person. The yield of MVK as given is based on the amount of formaldehyde in the feed to the reactor.
From the table, it is clear that the Aerolyst catalysts according to the invention has a much higher yield than the about 65% as reported in the Journal cjf Catalysis, and also has a higher yield than the 50% as found for the hydrotalcite catalyst. [Also, it is clear that a catalyst comprising not only Si02 but also AI2O3 - SA3235 - sho^s a high yield, albeit somewhat less than when a catalyst comprising only high-purity SJi02 is used. Furthermore, it is clear that an increase in the ratio of acetone to formaldehyde jeads to an increase of the selectivity towards MVK formation.

Claims
1. Process for the preparation of a ketone and/or an aldehyde, comprising the steps of:
a) forming a reaction mixture by bringing a starting ketone or a starting aldehyde or a mixture of a starting aldehyde and a starting ketone into the gaseous phase;
b) bringing the reaction mixture in contact with a catalyst, said catalyst comprising silica, said silica having a purity higher than 95 wt.%, whereby the ketone and/or the aldehyde is/are formed and whereby the reaction conditions are such that the conversion of at least the understoichiometrically present starting compound(s) is at least 50%.
2. Process according to claim 1, wherein the catalyst consists essentially of fumed silica having a purity higher than 98 wt.% and having a specific surface area lying between 25 and 500 m2/g,
3. Process according to claim 1 or 2, wherein the catalyst is essentially free of micropores.
4. Process according to any one of claims 1 - 3, wherein the starting ketone comprises acetone, the starting aldehyde comprises formaldehyde, and wherein in step a) the molar ratio between acetone and formaldehyde in the reaction;mixture lies between 9:1 and 100:1.
5. Process according to claim 1, wherein the reaction mixture comprises, at least at the moment it is brought in contact with the catalyst, between 1 and 50 wt.% water.
6. Process according to any one of claims 1 - 5, wherein the reaction mixture comprises, at least at the moment it is brought in contact with the catalyst, less than 10 wt.% of compounds other than compounds from the group consisting of aldehydes, ketones, stabilizers, and water.
7. Process according to any one of claims 1 - 6, wherein step b) is carried out ai a temperature lying between 250°C and 400º0.
8 Process according to claim 1, further comprising after step b) the steps of:
c) feeding the reaction mixture in the gaseout. phase to a rectification apparatus;
d) separating a top stream comprising the starting ketone and/or the starting aldehyde from the reaction mixture and removing it from the rectification apparatus;
e) recycling at least a portion of the lop stream to step a) or step b)
9. Process according to claim 8, wherein the starting ketone comprises acetone.
10. Process according to claim 9, wherein in step a» the reaction mixture comprises acetone and formaldehyde in a molar ratic lying between 9:1 and 100:1, wherein the ketone comprises methylvinylketone (MVK), said MVK being transferred into the liquid phase, whereby an MYK-stabilizing compound is mixed with MVK at the moment MVK is liquefied or shortly thereafter.
11. Process according to claim 10, wherein the MVK-stabilizing compound is a mixture comprising at least one of water, acetic acid, hydrochinone and acetonitrile.
12. Process for the preparation of vitamin A., comprising the process according to any one of claims 4 -11.
13. Process for the preparation of astaxanthin, comprising the process according to any one of claims 4 -11.
14. Process for the preparation of zeaxanthin, comprising the process according to any one of claims 4 -11.

Documents:

http://ipindiaonline.gov.in/patentsearch/GrantedSearch/viewdoc.aspx?id=U63qf912+w1OgkyJhIdSQA==&loc=+mN2fYxnTC4l0fUd8W4CAA==

« Previous Patent

Next Patent »

Patent Number

269196

Indian Patent Application Number

8244/DELNP/2008

PG Journal Number

41/2015

Publication Date

09-Oct-2015

Grant Date

08-Oct-2015

Date of Filing

30-Sep-2008

Name of Patentee

DSM IP ASSTS B.V.

Applicant Address

HET OVERLOON 1, NL-6411 TE HEERLEN, THE NETHERLANDS.

Inventors:

#	Inventor's Name	Inventor's Address
1	GUMMIN, INGOLF	STEINWEG 13, 79639 GRENZACH-WYHLEN, GERMANY.
2	HAEFELE, MARTIN	SALPETERERSTRASSE 29, 79713 BAD SACKINGEN, GERMANY.
3	NOESBERGER, PAUL	FRIEDHOFSTRASSE 7, CH-4127 BIRSFELDEN SWITZERLAND.

PCT International Classification Number

C07C 45/66

PCT International Application Number

PCT/EP2007/003233

PCT International Filing date

2007-04-12

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	06018055.1	2006-08-30	EUROPEAN UNION
2	06007691.6	2006-04-12	EUROPEAN UNION