METHOD FOR PRODUCTION OF METHYL METHACRYLATE

专利摘要:
method for producing methyl methacrylate. the present invention relates to a method for the production of methyl methacrylate, comprising the following steps: a) production of methacrylate and b) reaction of the methcrolein obtained in step a) in an oxidative esterification reaction in order to provide methyl methacrylate, characterized by the fact that both steps a) and b) occur in a liquid phase at a pressure of from 200 to 10000 kpa (2 to 100 bar), and step b) is carried out in the presence of a heterogeneous noble metal-containing catalyst comprising metals and/or comprising metal oxides.
公开号:BR112015025959B1
申请号:R112015025959-6
申请日:2014-04-11
公开日:2021-08-24
发明作者:Torsten Balduf；Martin Köstner；Matthias Grömping；Steffen Krill；Alexander LYGIN；Rudolf Burghardt
申请人:Röhm Gmbh；
IPC主号:

专利说明:

[0001] The present invention relates to a method for producing methyl methacrylate by direct oxidative esterification of methcrolein and the production of methcrolein.
[0002] Large amounts of methyl methacrylate are used for the production of polymers and copolymers with other polymerizable compounds. Methyl methacrylate is, moreover, an important building block for several methacrylic acid (MAA) esters of special characteristics, these being produced by transesterification with the corresponding alcohol.
[0003] Therefore it is highly desirable that the aforementioned starting material can be produced by a method which is as simple as possible, and has a good cost-benefit ratio in addition to protecting the environment.
[0004] Nowadays, methyl methacrylate (MMA) is mainly produced from hydrogen cyanide and acetone via the resulting acetone cyanhydrin (ACH) as the main intermediate. This method has the disadvantage of producing very large amounts of ammonium sulphate, the treatment of which incurs very high costs. Other methods that are not based on ACH are described in the relevant patent literature and are also carried out on a production scale. Among the raw materials used in this context as raw materials are those based on C-4 compounds, for example, isobutylene or tert-butanol, which are converted via a plurality of stages to the desired methacrylic acid derivatives.
[0005] The general procedure here is that isobutylene or tert-butanol is oxidized in a first stage to provide methcrolein, which is then reacted with oxygen to provide methacrylic acid. Methanol is then used to convert the resulting methacrylic acid to MMA. Further details of the above method are described, among others, in Ullmann's Encyclopedia of Industrial Chemistry 2012, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim, Methacrylic Acid and Derivatives, DOI: 10.1002/14356007.a16_441.pub2, and in Trends and Future of Monomer-MMA Technologies, SUMITOMO KAGAKU 2004- II.
[0006] Ethylene can also be used as a starting material instead of a C4 building block such as isobutylene in a variant of the above production method, and is first reacted with synthesis gas to provide propanal and then with formaldehyde to provide methacrolein. The resulting methcrolein is oxidized by air in the gas phase over a heterogeneous catalyst to provide methacrylic acid, which esterifies with methanol to provide MMA (Ullmann's Encyclopedia of Industrial Chemistry 2012, Methacrylic Acid from Ethylene, and Trends and Future of Ethylene Monomer-MMA Technologies, SUMITOMO KAGAKU 2004-II). This method has been operated since 1990 by BASF in a plant with a capacity of 40,000 metric tons per year for the production of methacrylic acid. According to the SUMITOMO article, this method was developed by BASF for specific requirements, and it is therefore difficult to make general use of said method for producing larger amounts of MMA.
[0007] Another method obtains MMA by oxidizing isobutylene or tert-butanol with atmospheric oxygen in the gas phase over a heterogeneous catalyst so as to provide methacrolein followed by using methanol in an oxidative esterification reaction of methacrolein. This method, developed by ASAHI, is described among others in US patent publications Nos. US 5,969,178 and US 7,012,039. This method is also described in the article by SUMITOMO, which provides detailed information on the disadvantages of said method, consisting in particular of high energy consumption, arising among others due to a non-pressurized procedure.
[0008] In addition, other problems associated with all the methods described above are in particular the relatively unsatisfactory production, high losses in the oxidation steps and the concomitant formation of CO2, and in general terms the concomitant formation of by-products that require complicated steps to isolating the product: all methods starting from isobutylene or from equivalent C-4 raw materials, such as TBA or MTBE, using gas phase oxidation over a heterogeneous catalyst system achieve yields below 90% , and the relevant literature describes yields below 85% for methacrolein production starting from isobutylene (eg Table 5 in Ullmann's Encyclopedia/Sumitomo, see above). The gas phase method proceeds naturally at moderate pressures of from 100 to 200 kPa (1 to 2 bar) absolute, and produces a method gas which comprises only about 4 to 6% by volume of the product component. Isolating the useful product from the inert gas ballast therefore incurs high energy costs and consumes large amounts of cooling energy as well as steam for multi-stage distillation elaboration steps.
[0009] The production of MMA according to the methods described so far produces relatively large amounts of waste, in particular exhaust gases or wastewater, which require costly disposal.
[0010] Conducting some of the methods described above, furthermore, requires a very complex plant, and therefore expensive, with associated high capital cost and high maintenance costs.
[0011] The above-cited review article from SUMITOMO describes the respective disadvantages in detail, and therefore may be incorporated herein into this patent application by way of reference.
[0012] Furthermore, Canadian Patent Application No. CN 101074192 describes a method of producing MMA in which methcrolein is first prepared from propanal and formaldehyde at a temperature in the range of 40 to 45°C and with a time of reaction in the range of 30 to 100 minutes, and is then oxidized with methanol to provide MMA. Furthermore, a similar method is proposed by Yuchao Li et al. "Synthesis of methacrolein by condensation of propionaldehyde with formaldehyde", Advance Materials Research Vols. 396-398 (2012). pp. 1094-1097. The aforementioned publication expressly advises the avoidance of operation at elevated temperature or superatmospheric pressure. The above method has the disadvantage of a high acid and amine requirement, these being used to catalyze the reaction. Consequently large amounts of waste products are produced, since a substantial proportion of the amine is destroyed under the mentioned conditions. One of the side reactions, which deactivates the catalyst, is the Eschweiler-Clarke reaction which leads to the formation of a methylated tertiary amine which is then not able to catalyze the Mannich reaction (US Patent No. 4,408,079 , column 2, lines 15 ff): by way of example, dimethylamine becomes trimethylamine.
[0013] In case, as described by Li, operations are then carried out at or around atmospheric pressure with large stoichiometric amounts of catalyst base, there is increased catalyst deactivation, and therefore the resulting procedure is not good cost-benefit ratio. These problems incur high costs which make the described method relatively uneconomical. The long reaction time resulting from conducting the unpressurized reaction is another serious disadvantage of both these methods.
[0014] European Patent Publication No. EP 0 890 569 discloses a method for producing methyl methacrylate by direct oxidative esterification of methcrolein with methanol. European Patent Publication No. EP 0 890 569 explicitly teaches here that a low water content of less than 2% by weight, preferably less than 1% by weight, in methacrolein is essential for oxidative esterification. The examples exclusively list reactions with a water content below 0.8% by weight. Furthermore, according to this teaching it is important that the total content of contaminants should be small. European Patent Publication No. EP 0 890 069 therefore teaches gas-phase oxidative methacrolein production from isobutylene with oxygen, and then complicated dehydration of the methacrolein in a column.
[0015] Although European Patent Publication No. EP 0 092 097 and German Patent Publication No. DE 28 55 504 teach an alternative synthesis method for methacrolein in the liquid phase, in a method in which propanal is reacted with formaldehyde, this method produces a large amount of water which, according to the teaching of European patent publication No. EP 0 890 569 makes this type of method unsuitable without complicated purification as a precursor stage for the oxidative esterification of methcrolein to methyl methacrylate. The starting materials and by-products used in this method, eg dimeric methacrolein, also potentially exert a detrimental or production-reducing effect in oxidative esterification, alongside the high water content: the product according to German patent publication No. DE 28 55 504 comprises more than 5% by weight of an aldol by-product which would be detrimental in oxidative esterification and would inevitably require complicated purification of metacrolein.
[0016] In light of the prior art, an object of the present invention is therefore to provide a technically improved MMA production method which does not have the disadvantages of conventional methods.
[0017] A particular objective is to enable the production of MMA with a relatively low energy use. Furthermore, the method must be carried out in a way that provides a high level of protection for the environment, so that the amounts of waste obtained are very small. A particular aim of the present invention is to increase the total MMA production, based on the raw materials used, for example by discovering and combining individual reaction steps with high product selectivity.
[0018] Furthermore, it should be possible to carry out the method with a very small number of steps, which should be simple and reproducible.
[0019] In addition, it should be possible to carry out the method using relatively simple and inexpensive plant. Therefore the capital expenditure for the plant must be small. Maintaining this plant should be simple and inexpensive.
[0020] Other purposes not explicitly mentioned are evident from the overall context of the description and claims in the parts that follow.
[0021] A method with all the features of patent claim 1 achieves the goals mentioned above, and also achieves other goals which are not explicitly mentioned, but which are readily derivable or deductible from the circumstances discussed in the introduction to this specification. Dependent claims 2 to 18 protect advantageous embodiments of the claimed MMA production method.
[0022] Therefore, the present invention provides a method for producing MMA, comprising the following steps: A) production of metacrolein from propanal and formaldehyde and B) reaction of the metacrolein obtained in step A) in an oxidative esterification reaction in order to provide MMA, which is characterized by the fact that the two steps A) and B) occur in a liquid phase at a pressure of from 200 to 10000 kPa (2 to 100 bar), and step B) is carried out in the presence of a heterogeneous noble metal-containing catalyst comprising metals and/or comprising metal oxides.
[0023] By virtue of the claimed method, it is possible, in an unpredictable way, to provide a method of producing MMA which does not have the disadvantages of conventional methods. Surprisingly, it has been seen here that, contrary to the general teaching of the prior art, steps A) and B) can also be combined without any complicated intervening purification or dehydration of the methcrolein, and lead to high yields of methyl methacrylate.
[0024] In particular, MMA can be produced with relatively low energy consumption. Furthermore, the method can be carried out in a manner that provides a high level of environmental protection, providing relatively small amounts of waste and substantially increasing atomic efficiency.
[0025] In particular, none of the reaction steps A) and B) in the claimed method require any additional water to be introduced into the reaction mixture and then in turn removed, and hence the total reaction volumes and rates of volume flow can be kept low.
[0026] The method can be, moreover, performed with relatively few steps, and these are simple and reproducible and proceed with relatively high productions of space-time.
[0027] The need for catalyst, in particular the need for organic base per metric ton of MMA produced, is furthermore very small.
[0028] In addition, the method can be performed with relatively simple and inexpensive plant. The capital expenditure for the plant is low. Maintenance of this plant is simple and inexpensive.
[0029] In this context it must be stated that, compared to the methods according to the prior art, the number of return flows and the magnitude of these have been reduced.
The by-products produced can, moreover, be removed very simply from the reaction mixtures, and the total method can therefore be carried out with high throughput, without any need for complicated purification steps. Step A)
[0031] The claimed method comprises the production of metacrolein. Suitable methods for this purpose are well known to persons skilled in the art and are the subject of relevant review articles, for example, in Ullmann's Encyclopedia of Industrial Chemistry 2012, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim, Acrolein and Methacrolein , DOI: 10.1002/14356007.a01_149.pub2.
[0032] The first stage of the method of the invention comprises the reaction of propanal with formalin in order to provide methacrolein.
[0033] Particularly suitable methods are those in which the total amount of separately added water or, respectively, water vapor during the conduct of the method is not more than 100% by mol, preferably 50% by mol, so particularly preferably 30% by mol, and most preferably 10% by mol, based in each case on methacrolein. The most suitable methods for producing methacrolein are those in which there is no reaction step in which water is separately added to the reaction mixture. The water introduced with the reactants and/or catalysts as well as the reaction water produced are excluded here.
[0034] However, surprisingly, the water content is not very relevant, or at concentrations of up to 5% by weight it has hardly any adverse effect on the oxidative esterification of step B). In light of the cited prior art it is therefore particularly surprising that the synthesis of methacrolein from propanal and formaldehyde can be combined with oxidative esterification, and indeed it is optionally possible to omit any dehydration after step A).
[0035] The reaction, which is carried out by means of an aldol condensation or a Mannich condensation, is not crucial per se. However, preferred methods are those which feature high production and low formation of by-products.
[0036] Therefore it is preferred to use reactions which have a selectivity of at least 80%, preferably at least 90% and particularly preferably at least 92%, based on the amount of propanal used.
[0037] Furthermore, preference is given to reactions which have a high production and high conversions by a single pass through the reaction zone. Preferred reactions feature a production and conversions of at least 80%, preferably at least 90% and particularly preferably at least 92%, based on the amount of propanal used.
[0038] Furthermore, it can be provided that the reaction according to step A) takes place with a molar ratio of propanal to formaldehyde which is preferably in the range of 2:1 to 1:2, particularly preferably of 1.5:1 to 1:1.5 and specifically preferably from 1.1:1 to 1:1.1. It is very particularly preferred to use an equimolar ratio of propanal to formaldehyde. It is therefore possible, in particular at high conversions, to omit any removal and return of propanal and/or formaldehyde from the mixture obtained after the reaction according to step A).
[0039] The reaction of propanal with formaldehyde generally uses catalysts, and several systems are known here which lead to a high production of methacrolein, with high selectivity.
[0040] Preferred methods for producing methacrolein starting from propanal and formaldehyde are described among others in U.S. Patent Publications No. US 7,141,702 ; German Patent Application No. DE 32 13 681 A1; U.S. Patent No. 4,408,079; United States Patent No. US 2,848,499; Japanese Patent Application No. JP 4173757A (Japanese Patent No. JP 19900300135); of Japanese Patent Application No. JP 3069420B2 and European Patent Application No. EP 0 317 909 A2, and for purposes relating to the disclosure of the teaching of the cited publications is hereby incorporated by reference into the present application.
[0041] The reaction of propanal with formaldehyde is carried out in the presence of acid, usually inorganic acid or organic mono-, di- or polycarboxylic acid, preferably monocarboxylic acid, in particular aliphatic monocarboxylic acid.
Advantageously used carboxylic acids are aliphatic monocarboxylic acids having 1 to 10, preferably 2 to 4, carbon atoms, or di- and polycarboxylic acids having 2 to 10, preferably 2 and 4 to 6 , carbon atoms. Dicarboxylic acids and polycarboxylic acids can be aromatic, araliphatic, and preferably aliphatic carboxylic acids. Suitable examples are acetic acid, propionic acid, methoxyacetic acid, n-butyric acid, isobutyric acid, oxalic acid, succinic acid, tartaric acid, glutaric acid, adipic acid, maleic acid, and fumaric acid. In principle, it is also possible to use other organic acids, but they are generally less advantageous for price reasons. Inorganic acids used are generally sulfuric acid and phosphoric acid. Mixtures of acids can also be used.
[0043] It is particularly preferred to use at least one organic acid for the reaction of propanal and formaldehyde, and even more preferably acetic acid.
[0044] The proportion of acid, based on propanal, is from 0.1 to 20% by mol, advantageously from 0.5 to 10% by mol, preferably from 1 to 5% by mol.
[0045] The reaction of propanal with formaldehyde is carried out in the presence of organic bases, preferably amines, particularly preferably secondary amines. Amines which can be used are preferably those of the formula R1R2NH, where R1 and R2are identical or different and are respectively an alkyl moiety having from 1 to 10, advantageously from 1 to 8, in particular from 1 to 4, carbon atoms, which may also be substituted by ether, hydroxy, or secondary or tertiary amino groups, in particular by from 1 to 2 of said groups, or are an aralkyl moiety having from 7 to 12 carbon atoms or a cycloalkyl moiety having from 5 to 7 carbon atoms, and R 1 and R 2 can also be, with the adjacent nitrogen, members of a heterocyclic ring, advantageously 5 to 7 members which can also comprise another nitrogen atom and/or an oxygen atom and the which may be substituted by hydroxyalkyl or alkyl groups having 1 to 4 carbon atoms.
[0046] Examples of amines that can be used are: dimethylamine, diethylamine, methylethylamine, methylpropylamine, dipropylamine, dibutylamine, diisopropylamine, di-isobutylamine, methylisopropylamine, methylisobutylamine, methyl-sec-butylamine, methyl(2-methylpentyl)amine, methyl(2-ethylhexyl)amine, pyrrolidine, piperidine, morpholine, N-methylpiperazine, N-hydroxyethylpiperazine, piperazine, hexamethyleneimine, diethanolamine, methylethanolamine, methylcyclohexylamine, methylcyclopentylamine, dicyclohexylamine or appropriate mixtures.
[0047] Furthermore, it can be provided that at least one of the amines used has no hydroxy group. It is particularly preferred that the proportion of amines having at least one hydroxy group is at most 50% by weight, preferably at most 30% by weight, and particularly preferably at most 10% by weight, based on the weight of the used amines.
[0048] The proportion of organic base, preferably secondary amines, is from 0.1 to 20% by mol, advantageously from 0.5 to 10% by mol, preferably from 1 to 5% mol based on propanal.
[0049] The ratio of amine equivalents to acid is preferably selected in such a way as to provide a resulting pH of from 2.5 to 9 in the reaction mixture prior to the reaction.
[0050] It can also be provided that the molar ratio of acid to organic base, preferably amine, is in the range of 20:1 to 1:20, preferably in the range of 10:1 to 1:10, so particularly preferably in the range of 5:1 to 1:5 and specifically preferably in the range of 2:1 to 1:2.
[0051] The reaction temperature for the reaction of propanal with formaldehyde at the exit of the reaction zone is from 100 to 300°C, preferably from 130 to 250°C, preferably from 140 to 220°C, in particular from 150 to 210°C.
[0052] The reaction pressure is in the range from 200 to 30000 kPa (2 to 300 bar), preferably from 500 to 25000 kPa (5 to 250 bar), particularly preferably from 1000 to 20000 kPa (10 to 200 bar), advantageously from 1500 to 15000 kPa (15 to 150 bar), preferably from 2000 to 10000 kPa (20 to 100 bar) and in particular from 4000 to 8000 kPa (40 to 80 bar). The pressure and temperature are adjusted in such a way that the reaction always takes place below the boiling point of the reaction mixture, ie the reaction proceeds in the liquid phase.
[0053] For the purposes of this application, all pressure data are absolute pressure in the unit kPa (bar).
[0054] The residence duration or the reaction time is preferably at most 25 minutes, advantageously from 0.01 to 25 minutes, more advantageously from 0.015 to 10 minutes, preferably from 0 .03 to 2 minutes. The dwell duration or the reaction time is particularly preferably in the range of 0.1 to 300 seconds, specifically preferably in the range of 1 to 30 seconds. It is advantageous to use a tubular reactor as a reactor for residence times below 10 minutes. Dwell duration here refers to the time for which the reaction mixture is reacted. All components are present here at reaction pressure and temperature, and the time referred to can therefore be calculated from the distance between the mixing point and the depressurization point. The depressurization point is the point at which the mixture is brought from the reaction pressure to a pressure below 500 kPa (5 bar).
[0055] The reaction mixtures may also comprise, in addition to water, organic solvents, for example, propanol, dioxane, tetrahydrofuran, and methoxyethanol.
[0056] Furthermore, it can be provided that the reaction of propanal with formaldehyde in order to provide methacrolein according to step A) takes place in the presence preferably at least 0.1% by weight, preferably at least 0.2 % by weight, and particularly preferably at least 0.5% by weight, of methanol, based on formalin. Despite the reported relatively high concentrations of methanol, by virtue of conducting the claimed reaction to the subsequent step B) it is possible to omit any complicated methanol removal in the formalin production and/or metacrolein purification stage.
[0057] According to a particular embodiment, formaldehyde and propanal can be mixed before said starting materials are brought up to reaction pressure and/or temperature.
[0058] The reaction can be carried out as follows: a mixture of propanal, amine, formaldehyde and advantageously water and/or acid and/or base is maintained at the reaction temperature and at the reaction pressure during the reaction time.
[0059] In a preferred embodiment, a mixture (advantageously equimolar mixture) of formaldehyde and propanal can be heated by means of a heat exchanger to the desired reaction temperature and passed into a tubular reactor. A catalyst solution (solution of the secondary amine and an acid, advantageously in H2O) optionally heated by means of a heat exchanger in the same way to the reaction temperature can be injected into the reactor inlet in the said mixture. A strongly exothermic reaction starts, and the temperature of the reaction mixture increases further. It is preferred that a pressure check valve at the exit of the reactor is used to maintain the pressure under which the reaction proceeds at such values that the reaction mixture still remains liquid during the reaction time, even when temperatures inside the reactor are high. After the reaction, the reaction mixture can be depressurized to atmospheric pressure and worked up. In the production of methacrolein from propanal and formaldehyde it is preferred that the reaction mixture be passed into a column for steam stripping. Methacrolein is discharged along with water at the top of the column. The mixture is condensed and separated by means of a phase separator to provide an upper phase and a lower phase. The upper phase comprises methacrolein, and is reacted by oxidative esterification according to step B) to provide MMA. The lower phase is mainly made up of water. Preferably it in turn can be at least to some extent returned to the column in order to remove residual metacrolein dissolved therein.
[0060] The aqueous solution of catalyst can be extracted at the bottom of the column together with the water formed in the reaction and the water from the formaldehyde solution. For the purposes of further processing, the liquid from the bottom of the column can be discarded if too little amine and/or too little acid is used, and catalyst backflow therefore does not pay.
[0061] However, in the case of higher concentrations of amine and/or acid in the material discharged to the bottom of the column, it is also possible to carry out distillation removal of water at least to some extent and in turn return the catalyst solution to the reactor. Another possibility is to split the discharged material at the bottom of the column into two substreams on one moto such that one substream precisely comprises the amount of water that was formed during the reaction and introduced with the starting materials. The referred underflow is then removed from the system, and the remaining proportion is returned to the reactor. Aqueous and propanal formaldehyde can also be separately preheated and introduced into the reactor.
[0062] Propanal used for the production of metacrolein can be purchased in large quantities. Said compound can preferably be obtained by reacting ethylene with carbon monoxide (CO) and hydrogen (H2). The hydroformylation reaction generally performed for this purpose is well known, and reference is made in this context to standard literature, for example, Kirk-Othmer Encyclopedia of Chemical Technology, John Wiley & Sons, Inc., OXO Process and Franke et al. , Applied Hydroformylation, dx.doi.org/10.1021/cr3001803, Chem. Rev. 2012, 112, 5675-5732; the publications referred to are hereby incorporated by reference into the present application.
[0063] Catalysts are generally used for this reaction. Among the preferred catalysts are in particular compounds in which rhodium, iridium, palladium and/or cobalt are present, with particular preference being given here to rhodium.
[0064] According to a particular modality, it is in particular possible to use, for catalysis, complexes which comprise at least one compound containing phosphorus as a ligand. Preferred phosphorus-containing compounds comprise aromatic groups and at least one, particularly preferably two phosphorus atoms. Among the phosphorus-containing compounds are in particular phosphines, phosphites, phosphinites, phosphonites. Examples of phosphines are triphenylphosphine, tris(p-tolyl)phosphine, tris(m-tolyl)phosphine, tris(o-tolyl)phosphine, tris(p-methoxyphenyl)phosphine, tris(p-dimethylaminophenyl)phosphine, tricyclohexylphosphine, tricyclopentylphosphine, triethylphosphine, tri(1-naphthyl)phosphine, tribenzylphosphine, tri-n-butylphosphine, tri-t-butylphosphine. Examples of phosphites are trimethyl phosphite, triethyl phosphite, tri-n-propyl phosphite, tri-i-propyl phosphite, tri-n-butyl phosphite, triisobutyl phosphite, tri-tert-butyl phosphite, tris(2-ethyl-hexyl) phosphite , triphenyl phosphite, tris(2,4-di-tert-butylphenyl) phosphite, tris(2-tert-butyl-4-methoxyphenyl) phosphite, tris(2-tert-butyl-4-methylphenyl) phosphite, tris(p- cresyl) phosphite. Examples of phosphonites are methyldiethoxyphosphine, phenyldimethoxyphosphine, phenyldiphenoxyphosphine, 2-phenoxy-2H-dibenzo[c,e][1,2]oxaphosphorine and its derivatives in which some or all of the hydrogen atoms have been replaced by alkyl and/or aryl moieties or halogen atoms. Commonly used phosphinite binders are diphenyl(phenoxy)phosphine and its derivatives, diphenyl(methoxy)phosphine and diphenyl(ethoxy)phosphine.
[0065] Catalysts and binders for the hydroformylation method are described by way of example in International Patent Application Publication No. WO 2010/030339 A1 , WO 2008/071508 A1 , European Patent Application Publication No. EP 982 314 B1, in International Patent Application Publication No. WO 2008/012128 A1, WO 2008/006633 A1, in International Patent Application Publication No. WO 2007/036424 A1, in International Patent Application Publication No. WO 2007/ 028660 A1, in International Patent Application Publication No. WO 2005/090276 A1, and for purposes of disclosure reference is made to said publications, and the catalysts and binders disclosed therein are incorporated in this application. The publications referred to also describe reaction conditions, which are also incorporated in the present application.
[0066] The hydroformylation of ethene uses carbon monoxide and hydrogen, usually in the form of a mixture known as synthesis gas. The composition of the synthesis gas used for the hydroformylation method can vary widely. The molar ratio of carbon monoxide and hydrogen is generally from 2:1 to 1:2, in particular around 45:55 to 50:50.
[0067] The temperature in the hydroformylation reaction is generally in the range of about 50 to 200°C, preferably about 60 to 190°C, in particular about 90 to 190°C. The reaction is preferably carried out at a pressure in the range of about 500 to 70000 kPa (5 to 700 bar), preferably 1000 to 20000 kPa (10 to 200 bar), in particular 1500 to 6000 kPa (15 to 60 Pub). The reaction pressure can be varied depending on the activity of the hydroformylation catalyst used.
[0068] Pressure resistant reaction equipment suitable for the hydroformylation method are known to the person skilled in the art. Among these are general knowledge reactors for gas-liquid reactions, eg gas circulation reactors, bubble columns, etc., which may optionally have internal divisions.
[0069] Other preferred embodiments of a hydroformylation reaction are described inter alia in European Patent Application Publication No. EP 1 294 668 B1, and the contents of said publication are hereby incorporated by reference into the present application.
[0070] According to a particularly preferred embodiment, methacrolein can be produced from propanal and formaldehyde in a tandem reaction where propanal is obtained by the reaction of ethylene, carbon monoxide and hydrogen and is reacted directly with formaldehyde. This method is described in detail by Deshpande et al., Biphasic catalysis for a selective oxo-Mannich tandem synthesis of methacrolein, Journal of Molecular Catalysis A: Chemical 211 (2004) 49-53, doi:10.1016/j.molcata.2003.10. 010, and US Patent Application Publication No. 7,141,702 B2, and said publications are hereby incorporated by reference into the present application. Step B)
[0071] According to the invention, the metacrolein obtained in step A) is reacted in a direct oxidative esterification reaction in order to provide MMA.
[0072] For the purposes of the present invention, a direct oxidative esterification reaction is a method in which methcrolein is reacted directly, that is, without formation of large amounts of methacrylic acid, in order to provide MMA in the presence of methanol and a oxidant, preferably oxygen.
[0073] In contrast to this, in methods which are carried out by way of example by BASF, methcrolein is first oxidized to provide methacrylic acid, which is then esterified in a further reaction step with methanol to provide MMA .
[0074] In the method according to BASF it is possible that methanol present for stabilization purposes or present by virtue of the production method in the formaldehyde used similarly forms small amounts of MMA during the oxidation of methacrolein. However, this MMA cannot be separated from the returned methacrolein by cheap purification methods, and it usually decomposes under selected conditions; this, therefore, reduces the final production of MMA from methanol present in formaldehyde. In order to solve this problem, a complicated method to release formaldehyde from methanol must be used. Alternatively, it is certainly possible to use a purification step to remove the MMA present in the composition intended for return, but both solutions incur a high cost, which is uneconomical because the amounts of MMA obtained are relatively small.
[0075] The oxidation of methacrolein in an oxidative esterification reaction according to step B) of the method of the present invention generally yields at most 30% by weight, preferably at most 15% by weight, particularly preferably at most 5% by weight of methacrylic acid.
[0076] An oxidative esterification reaction is carried out with an oxidant, and it is preferable to use oxygen (O2) for this purpose. For cost reasons, air can be used preferentially, and it can comprise different proportions of oxygen; this would not be crucial to the present invention.
[0077] At least one heterogeneous oxidation catalyst is further used to carry out a reaction according to step B), and these selectively accelerate the oxidation reaction defined in more detail above. Suitable catalysts are well known to those skilled in the art and are described by way of example in European Patent Application Publication Nos. EP 0 857 512 A1 , EP 1 393 800 A1 , EP 2 177 267 A1 , and EP 2 210 664 A1 , and reference is made to the publications referred to for purposes of disclosure, and the catalysts disclosed therein are incorporated in this application. The publications referred to also describe reaction conditions, which are also incorporated in the present application.
[0078] Heterogeneous oxidation catalysts preferably comprise at least one noble metal and/or at least one metal oxide. Preference is given here to oxidation catalysts in which gold and/or palladium and/or ruthenium and/or rhodium and/or silver is or is present. Catalysts containing gold and/or palladium are particularly preferred.
[0079] Among the catalysts suitable for carrying out the present method are among other palladium catalysts, where these preferably comprise palladium and lead and are generally used on a support.
[0080] A palladium catalyst may also comprise at least one compound selected from the group consisting of an alkali metal compound and an alkaline earth metal compound. It is preferred that a palladium catalyst comprises from 0.01 to 30% by weight, more advantageously from 0.01 to 5% by weight, of at least one compound selected from the group consisting of a compound of alkali metal and an alkaline earth metal compound.
[0081] The introduction of the alkali metal compound and/or the alkaline earth metal compound into the catalyst can be carried out by a method in which such a compound is added to a solution in which a palladium compound and/or a palladium compound. lead is present, and a support is treated with the solution, whereby the alkali metal compound and/or the alkaline earth metal compound, together with the palladium compound and/or the lead compound, is adsorbed onto support or adhere to this. Alternatively, a support which comprises an alkali metal compound and/or an alkaline earth metal compound adsorbed thereon can be used for producing a catalyst. Another possibility, instead of using a support, is that a solution in which an alkali metal compound and/or an alkaline earth metal compound is present is added to the reaction mixture during the reaction according to step B).
[0082] The amount of palladium supported on the support is not subject to any particular restriction, but the amount is preferably from 0.1 to 20% by weight, more preferably from 1 to 10% by weight, based on the weight of the bracket. The amount of lead supported on the support is not subject to any particular restriction, but the amount is preferably from 0.05 to 17% by weight, more preferably from 0.45 to 8.5 % by weight, based on the weight of the holder. The atomic ratio of palladium to lead is preferably in the range 3:0.7 to 3:1.3, more preferably in the range 3:0.9 to 3:1.1.
[0083] A disadvantage of the palladium catalysts described above is that lead generally present can cause environmental damage and therefore wastewater requires complicated treatment to remove lead residue.
[0084] In an alternative embodiment, a catalyst used for oxidative esterification comprises minimized amounts of lead. Therefore, the oxidative esterification reaction according to step B) can be carried out using a catalyst of which the lead content is preferably at most 20% by weight, preferably at most 10% by weight, specifically preferably at most 5% by weight, particularly preferably at most 2% by weight and most particularly preferably at most 1% by weight. According to a specifically preferred embodiment, step B) uses a catalyst which preferably comprises at most 1.5% by weight, preferably at most 1% by weight, specifically preferably at most 0.5% by weight weight, particularly preferably at most 0.2% by weight and most particularly preferably at most 0.1% by weight, of lead. Step B) can furthermore use a catalyst which does not comprise any measurable lead content.
[0085] It can also be provided that the oxidative esterification reaction according to step B) is carried out using a catalyst which comprises one or more metals selected from the group consisting of gold and/or palladium and/or ruthenium and /or rhodium and/or silver. It is preferred that said metals take the form of ultra-finely dispersed metals, i.e. they take the form of nanoparticles, applied to a support. The average diameter of the metal particles is preferably at most 20 nm, preferably at most 10 nm, particularly preferably 5 nm, where said value is based on a numerical average determined by TEM (Electronic Microscopy by Transmission (Transmission Electron Microscopy)). The "average diameter" of the particles is calculated from the diameter of 100 particles selected from 120 particles, where the ten largest particles and the ten smallest particles of the 120 particles are ignored.
[0086] A preferred catalyst may comprise other catalytically active constituents alongside gold particles and/or palladium particles and/or ruthenium particles and/or rhodium particles and/or silver particles. Among the other catalytically active constituents are among others magnesium, scandium, yttrium, lanthanum and other lanthanides with atomic numbers from 58 to 71, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron , osmium, cobalt, iridium, nickel, platinum, copper, zinc, cadmium, aluminum, gallium, indium, thallium, germanium, tin, lead, antimony, and bismuth, these being capable of being respectively present in metallic and/or oxidized form (for example, in the form of oxides, hydroxides, or salts). The other catalytically active constituents mentioned take the form of particles which preferably have an average diameter of at most 20 nm, preferably at most 10 nm, particularly preferably at most 5 nm. It is possible here that gold particles and/or palladium particles and/or ruthenium particles and/or rhodium particles and/or silver particles and particles with other catalytically active constituents are present together or separately, in particular in alloyed form or unalloyed form, on the support. It is preferred that the gold particles and/or the palladium particles and/or the ruthenium particles and/or the rhodium particles and/or the silver particles comprise the other catalytically active constituents.
[0087] The proportion of catalytically active particles in the catalyst can vary widely. The proportions of the catalytically active particles are preferably in the range of about 0.01 to 20 parts by weight, particularly preferably in the range of 0.1 to 10 parts by weight, per 100 parts by weight of catalyst.
[0088] If the catalyst comprises, along with gold particles, other elements in the form of catalytically active components, the atomic ratio of gold to all other elements may be in the range of 1:0.001 to 1:1000, of preferably from 1:0.01 to 1:100, particularly preferably from 1:0.1 to 1:10 and specifically preferably from 1:0.2 to 1:5.
[0089] In addition, it can be provided that the oxidative esterification reaction according to step B) is carried out using a nickel-containing catalyst. It is preferred that nickel-containing catalysts comprise a noble metal content, preferably gold. It is preferred that nickel-containing catalysts comprise nickel oxide, which is used in combination with nickel, palladium, platinum, ruthenium, gold, silver and/or copper. It is preferred that the atomic ratio of NiOx to (NiOx + X) is in the range from 0.20 to 0.99, preferably from 0.30 to 0.90 and particularly preferably from 0.50 to 0.90, where X is selected from nickel, palladium, platinum, ruthenium, gold, silver and/or copper, with particular preference given here to gold. In this formula, NiOx is present as an oxide, while X is present as a metallic form.
[0090] Nickel oxide (NiOx), by way of example, may take the form of Ni2O, NiO, NiO2, Ni3O4 or Ni2O3.
[0091] Nickel oxide and other components, in particular metallic components, such as nickel, palladium, platinum, ruthenium, gold, silver and/or copper, can be used here preferably in the form of nanoparticles with a size in the range from 2 to 15 nm, preferably from 2 to 10 nm and particularly preferably from 2 to 6 nm, where this value refers to a numerical mean determined by TEM (Transmission Electron Microscopy), as defined in more detail above. The nanoparticles are preferably fixed on a support.
[0092] The catalysts described above are generally applied on a support, where said supports may comprise metal oxides (for example, silicon dioxide, aluminum oxide, titanium oxide, zirconium oxide, or magnesium oxide), oxides mixed (such as silicon dioxide - aluminum oxide, titanium dioxide - silicon dioxide or silicon dioxide - magnesium oxide), zeolites (such as ZSM-5), mesoporous silicates (such as MCM41), natural minerals (such as such as clay, diatomaceous earth, or pumice), or carbon materials (eg, activated charcoal or graphite). It is preferable to use oxide-based inorganic supports.
[0093] It is particularly advantageous to use an inorganic support based on oxides and comprising silicon, lithium, sodium, potassium, magnesium, calcium, scandium, yttrium, lanthanum and other lanthanides with atomic numbers from 58 to 71, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, platinum, palladium, copper, silver, zinc, cadmium, boron, aluminum, gallium, indium, thallium, germanium, tin, lead, antimony, bismuth and/or tellurium.
[0094] A preferred oxide-based support comprises silicon oxide as a major component and one or more members of the group consisting of lithium, sodium, potassium, magnesium, calcium, scandium, yttrium, lanthanum and other lanthanides with atomic numbers from 58 to 71, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, copper, silver, zinc, cadmium, aluminum, gallium, indium, thallium, germanium, tin, lead, antimony and bismuth.
[0095] The method for producing the aforementioned inorganic supports based on oxides is not subject to any particular restrictions, and it is possible to use any known production method. Examples include impregnation, coprecipitation, ion exchange, gas phase deposition, kneading and hydrothermal synthesis.
[0096] It is preferred to use a porous support. It is particularly preferred that the specific surface area (BET method) is generally at least 50 m2/g, preferably at least 100 m2/g.
[0097] The method for loading the support with the catalytically active constituents is not subject to any particular restrictions. Suitable methods are among others co-precipitation, precipitative deposition, impregnation and vapor phase deposition.
[0098] The catalysts described above based on gold and/or nickel oxide are preferred over palladium catalysts. Nickel-containing and gold-containing catalysts may preferably be lead-free.
It can preferably be provided that the water content of the reaction mixture used for the oxidative esterification in step B) is preferably at most 10% by weight and preferably at most 5% by weight.
[00100] Said low proportions of water can optionally be obtained using a phase separator, and the water content of the methcrolein phase can vary here as a function of temperature. Therefore, it is preferable that the reaction mixture obtained after the reaction of formaldehyde with propanal is cooled to a temperature at which the water content in the metacrolein phase adopts the mentioned values. The temperature in the phase separator can be preferably set from 0 to 50°C, preferably from 5 to 30°C and particularly preferably from 10 to 25°C. However, dewatering is only necessary at particularly high water contents of more than 10% by weight, to the extent that a notable increase in space-time production can be obtained. In the case of water contents above 5% by weight, a small increase in the production of methyl methacrylate can be obtained by removing the water until the content is below 5% by weight.
[00101] Equally surprisingly, it was seen that, contrary to the hypotheses made in the prior art, high space-time yields of methyl methacrylate can also be obtained with residual content of starting materials or by-products from step A): although propanal, formaldehyde and dimeric methcrolein are reacted to provide methyl propionate, methyl formate and the oxidized dimeric methcrolein methyl ester, this formation of by-products is the only adverse effect of these components on the entire method. Surprisingly, therefore, the total MMA production is very high, and the mentioned by-products can be easily removed during MMA elaboration.
[00102] Furthermore, it is preferred that the content of methacrolein in the reaction mixture used for the oxidative esterification in step B) is at least 5% by weight, preferably at least 15% by weight and particularly preferably in the minimum 25% by weight.
[00103] It can also be provided that the oxidative esterification reaction according to step B) preferably takes place with a molar ratio of methanol to methcrolein in the range of 1:1 to 50:1, particularly preferably of 1, 5:1 to 25:1 and specifically preferably from 2:1 to 10:1.
[00104] The amount of catalyst to be used varies depending on the composition of the feed and catalyst mixture, the reaction conditions, and the types of reaction and the like. If the catalyst used takes the form of a slurry, it is preferred that the amount of catalyst used is from 0.01 to 0.5 kg/l of the reaction system solution.
[00105] The oxidative esterification reaction can be carried out in any conventional manner, for example, in a liquid phase reaction or in a drip bed reaction. By way of example, it is possible to use any known reactor, for example a bubble column reactor, a tubular reactor with air flow or an agitated reactor.
[00106] The pressure at which the reaction referred to is carried out can vary widely. Surprising advantages can be obtained through a reaction pressure in the range from 200 to 10000 kPa (2 to 100 bar), preferably from 300 to 8000 kPa (3 to 80 bar), more preferably from 400 to 5000 kPa ( 4 to 50 bar) and particularly preferably from 500 to 2000 kPa (5 to 20 bar).
[00107] It is preferable to maintain the reaction system at a pH of from 5 to 9, particularly from 6.5 to 8, adding at least one basic compound preferably selected from the group consisting of an alkali metal compound and/or an alkaline earth metal compound, for example an oxide, hydroxide, carbonate, carboxylate or the like.
[00108] The oxidative esterification reaction according to step B) can take place at a temperature preferably in the range from 10°C to 200°C, particularly preferably from 40 to 150°C and particularly preferably from 60 to 120°C.
[00109] The reaction time or duration of residence varies depending on other reaction conditions; however, preferably it is in the range of 10 minutes to 48 hours, more preferably 30 minutes to 24 hours and particularly preferably 45 minutes to 2 hours.
[00110] Additional information regarding conducting an oxidative esterification reaction according to step B) for MMA synthesis is found among others in United States patent publication No. US 4,249,019 or in German patent application publication No. DE 3018071A1.
[00111] Oxidative esterification under the conditions mentioned above provides a reaction mixture which comprises MMA as the main reaction product. The resulting reaction mixture also comprises, in addition to MMA, unreacted methcrolein and unreacted methanol and small amounts of water and methacrylic acid as by-products. The reaction mixture also comprises trace amounts of other by-products which comprise dimethacrolein and the like.
[00112] The reaction product obtained in step B) can be prepared in a known way in order to obtain pure MMA: the reacted reaction mixture obtained through oxidative esterification according to step B) can be first prepared by distillation.
[00113] According to a preferred embodiment, the reaction mixture can be passed into a distillation tower, and preferably is passed into the central portion thereof: generally it is possible to discharge an azeotropic mixture of methcrolein and methanol as a product of high distillation.
[00114] A mixture comprising liquid MMA, methanol, water and other by-products is obtained from the bottom of the distillation tower. Said liquid mixture is purified by a conventional method. Said purification unit can generally comprise at least one, preferably two or more, distillation systems for removing high-boiling and low-boiling compounds.
[00115] In the present invention, the nature of the distillation tower that is preferably used for preparing the reaction mixture obtained from the oxidative esterification is not subject to any particular restriction, and it is possible to use any desired conventional distillation tower , for example, a plate column or a loaded column.
[00116] However, as methcrolein, MMA and methacrylic acid, which are passed into the distillation tower, are readily polymerizable compounds, it is preferable to use a distillation system with a structure where no blocking by polymerization products and/ or polymerization products can be easily removed. Specific examples of distillation towers comprise plate columns equipped with a sieve tray, cascade tray, turbogrid tray, slotted tray or the like, and columns loaded with ordered loading materials (eg Mellapak from Sulzer) or with materials of disordered loading (eg Raschig Superring from Raschig).
[00117] The proper distillation temperature in the distillation tower preferably used in the claimed method for preparing the reaction mixture obtained from the oxidative esterification varies as a function of the distillation pressure, the composition of the liquid in the distillation tower, the number of plates in the distillation tower and the like. However, in order to minimize the formation of the polymerization products mentioned above and the formation of high boiling compounds which represent a production loss, based on methacrolein or MMA, it is preferable that the distillation temperature is minimized. However, if too low a distillation temperature is selected, disadvantages can arise. Among these, by way of example, is that a low distillation pressure must also be selected. This may require the use of a disadvantageously large distillation tower. In addition, it may be necessary to use a coolant to concentrate the gas phase in the upper portion of the distillation tower. It is preferred that the distillation temperature, or the temperature of the liquid in the column, is in the range of 20 to 100°C, particularly 40 to 85°C. The distillation pressure is calculated from the stated temperature.
[00118] As previously mentioned, methacrolein, MMA and optionally other polymerizable by-products, such as methacrylic acid, can be passed into a distillation tower in order to separate the product of the oxidative esterification reaction into methanol/methacrolein mixtures and mixtures of MMA/water.
[00119] As polymers can be formed, it is preferred that one or more polymerization inhibitors are added to the method. Polymerization inhibitors are well known to those skilled in the art, examples being hydroquinones, hydroquinone ethers such as hydroquinone monomethyl ether or di-tert-butylpyrocatechol, phenothiazine, N,N'-diphenyl-p-phenylenediamine, 4-hydroxy - 2,2,6, 6-tetramethylpiperidin-1-oxyl, p-phenylenediamine, methylene blue and sterically hindered phenols. The compounds mentioned can be used individually or in the form of mixtures and are generally commercially available. The action of stabilizers mainly consists of their action as free radical scavengers for free radicals arising from polymerization. Reference is made to the familiar technical literature for further details, in particular the Rompp-Lexikon Chemie [Rompp's Chemical Encyclopedia]; Editors: J. Falbe, M. Regitz; Stuttgart, New York; 10th Edition (1996); keyword "Antioxidantien" and the references cited therein.
[00120] In particular, phenols are preferably used as polymerization inhibitor. Particularly surprising advantages can be obtained when using hydroquinone monomethyl ether. The proportion of the inhibitors, individually or as a mixture, can generally be from 0.001 to 0.5% by weight, based on the weight of the entire composition.
[00121] It is preferred that steps A) and B) be carried out in a continuous method. The introduction of starting materials into the plant for carrying out a method according to the present invention, and the removal of products from the plant, here occurs continuously for any desired period. However, this period may be interrupted for maintenance and repair work.
[00122] Furthermore, it can be provided that the reactor volume in step A) is smaller than the reactor volume in step B). The reactor volume here is based on the volumes in step A) and step B), where the starting materials used within these are reacted in the liquid phase under the high pressure of the respective reaction in order to provide the products.
[00123] The ratio of the reactor volume in step A) to the reactor volume in step B) is advantageously in the range of 1:1000 to 1:100, preferably in the range of 1:800 to 1:200 and particularly preferred mode in the range of 1:500 to 1:300.
[00124] Typical reactor volumes for a continuously operated production plant can be, by way of example, for step A) a tube/tube-bundle reactor with capacity from 0.1 to 0.5 m3 and for step B) a tubular/tube bundle reactor with capacity from 10 to 15 m3 or a continuously operated stirred tank of capacity from 50 to 100 m3, but this data is not intended to represent any restriction.
[00125] Surprisingly, when the present method is compared with conventional methods which oxidize C4 building blocks such as isobutylene, it successfully obtains a remarkable reduction in the volume to be compressed, in particular of gas.
[00126] In the claimed method, composed of the combination of reaction steps A) and B), there is no essential requirement in any of the individual reaction steps to introduce additional water into the reaction mixture, i.e., water that is no longer present due to other circumstances in the reagents. This is a decisive advantage over the prior art, since introduced water additionally increases the reaction flows and therefore also increases the necessary equipment, and generally also in turn requires removal of the desired end products, at energy cost. resulting additional and other costs. Total reaction volumes and volume flow rates can therefore be kept low in the claimed method.
[00127] The Asahi method according to United States Patent Publication No. US 5,969,178 and United States Patent Publication No. US 7,012,039 requires by way of example during the oxidation of the C4 component of the gas phase the addition and in turn subsequent removal of a schematic excess of water. The methods known to date for producing methacrolein from ethylene via propionaldehyde, then oxidizing this to methacrylic acid and then esterifying to MMA require the addition of a skechiometric excess of water during the oxidation of methcrolein to methacrylic acid from gas phase to ensure that the activity of the oxidation catalyst is maintained.
[00128] In the claimed method, composed of the combination of reaction steps A) and B), the total amount of water separately added during the conduction of the reaction is therefore not more than 100% by mol, preferably 50% by mol , particularly preferably 30% by mol, and even more preferably not more than 10% by mol, based in each case on methacrolein. In a particularly advantageous embodiment of the claimed method, no water is separately added to the reaction mixture in any of the reaction steps A) and B) during the conduct of the reaction. Reaction water and water addition for elaboration steps are always excluded here.
[00129] Figure 1 is by way of example a diagram of the claimed method, but is not intended to restrict the invention.
[00130] Formaldehyde (FA) and propanal (PA) are introduced after pre-mixing or individually into reactor 1, and similarly the organic base (OB) and the acid catalyst (A) are introduced after pre- mixture or individually inside the reactor. After aldol condensation and catalyst removal, methacrolein (MAL) is isolated. The catalyst can be returned to reactor 1 via flow (1). MAL and methanol (MeOH) are introduced into the oxidative esterification reactor (DOE reactor). A gas containing oxygen (O2) is introduced into the aforementioned reactor. Unreacted MAL from the esterification reactor is removed as a MAL/methanol azeotrope in an MMA/water-MAL/MeOH separation method, and is returned to the DOE reactor via flow (2). Then follows a method of separating MMA/water and further purifying the raw MMA.
[00131] Figure 2 shows a possible system for the reaction of formaldehyde with propanal in order to provide methacrolein (step A). Aqueous formalin 101 is mixed with propionaldehyde 102 and passed in the form of stream 103 into the preheater 11. Dimethylamine (40% aqueous solution) 104 and acetic acid 105 are mixed and passed in the form of stream 106 into the preheater 12 Operation of preheaters 11 and 12 is optional. The mixture from the outlets 11 and 12 is introduced in the form of flow 107 into the tubular reactor 13. The tubular reactor 13 is heated by means of an oil bath to the reaction temperature. Downstream of the tubular reactor, the mixture 108 is depressurized at valve 14 and introduced into column 15. The material discharged from the bottom of the column is split 50/50, and a portion is returned to flow 107 into reactor 13. the other portion being passed for disposal as a stream from the wastewater stream 112. The stream obtained at the top of the column is condensed in the condenser 16 and is introduced as stream 109 into the phase separator 17. A methcrolein rich phase 111 in the said phase separator is discharged as product into the "direct oxidative esterification" portion of the system according to Figure 3, and the stream 111 here can optionally be dried by azeotropic distillation (not shown) . The aqueous discharge from phase separator 17 is returned as flow 110 to column 15.
[00132] Figure 3 shows a possible equipment which can produce MMA from MAL and which is suitable to carry out direct oxidative esterification (step B). Methanol is introduced via supply line 200 to line 111 whereby methcrolein is withdrawn from step A) of the method. Air (or oxygen-containing gas mixture) is passed through supply line 202 into reactor 21, which comprises a catalyst suitable for the direct oxidative esterification method, and a basic composition which preferably comprises methanol and NaOH it is also passed through supply line 203 into reactor 21 in order to adjust the pH. Figure 3 does not show accessory assemblies such as pumps, heating elements, heat exchangers and condensers. Furthermore, it is optionally possible to use a plurality of reactors 21 connected in series (not shown).
[00133] Exhaust gases are discharged from reactor 21 through the exhaust gas purifier via line 204, and methanol, MMA and methcrolein here can be, at least to some extent, condensed in one or more condensers and returned to the reactor 21 (not shown).
[00134] The reaction mixture present in reactor 21 is passed through line 205 to distillation column 22, and methacrolein (or mixture containing methacrolein) here is returned through line 206 to reactor 21. Gases and other components low boiling point can be removed from the reaction mixture at the top of distillation column 22 and introduced through line 207 into the exhaust gas. The composition taken via line 209 from the material at the bottom of distillation column 22 in essence comprises MMA, which may comprise methanol, methacrylic acid, sodium methacrylate and other components.
[00135] An acid or acid containing mixture, for example aqueous sulfuric acid, may be passed through supply line 208 from a feed vessel to line 209. The resulting mixture is passed to a water/oil separation system 23 which by way of example may comprise a centrifuge, and is separated into aqueous and organic phase. At this point it is possible to connect a plurality of similar oil/water separation systems in parallel so that these can be operated alternately as needed (not shown). The aqueous phase from separation system 23 can be introduced via line 210 into a wastewater treatment system, while the organic phase is introduced via line 211 into distillation column 24 for removal of high components. boiling point. High boiling components, e.g. methacrylic acid, can be taken from the material at the bottom of said column 24 via line 212 for further post-treatment. Raw MMA is withdrawn from the top of column 24 via line 213 and introduced into column 25. Low boiling components (eg methanol and methacrolein) can be withdrawn from the top of said column via line 215 and returned via line 218 to reactor 21, and a portion thereof may be discharged and introduced into exhaust gas stream 204. Purified MMA may be withdrawn from material at the bottom of column 25 via line 214 and can be introduced into the final column for purification of MMA 26. Pure MMA is withdrawn from the top of the column via line 217, while the remaining high-boiling components can be withdrawn from material at the bottom of the column via line 216 for post-treatment or for return upstream from column 24 (not shown). Key Figure 1 OB Organic base A Acid MeOH Methanol O2 Oxygen-containing gas MMA Methyl methacrylate FA Formalin (aqueous formaldehyde solution) PA Propanal MAL Metacrolein DOE Direct oxidative esterification Catalyst return Methacrolein/methanol return Figure 2 FOL Formalin (aqueous solution of formaldehyde) PA Propanal DMA Aqueous solution of dimethylamine AcOH Acetic acid MAL Methacrolein 11 Heat exchanger (preheater) 12 Heat exchanger (preheater) 13 Reactor (tubular reactor) 14 Pressure holding valve 15 MAL distillation column 16 Condenser 17 Separator phases 101 Aqueous formalin line 102 Propanal line 103 Line leading to heat exchanger 104 Dimethylamine line (40 % aqueous solution) 105 Acetic acid line 106 Line leading to heat exchanger 107 Line leading to reactor 108 Line taking product mixture to column 109 Condensate line 110 Return to column 111 MAL to stage B) 112 Line taking to to the wastewater system 113 Return of discharged material from the bottom of the column Figure 3 MAL Methacrolein MeOH Methanol O2 Oxygen gas MMA Methyl methacrylate 21 Reactor 22 Removal of MAL 23 Water/oil separation 24 Removal of high point materials boiling 25 Removal of low boiling material 26 Final purification of MMA 111 MAL from stage A) 200 MAL/methanol supply line 202 MAL/methanol supply line 202 Oxygen-containing gas supply line 203 Base composition supply line 204 Exhaust gas flow 205 Product flow to column 22 206 MAL return 207 Exhaust gas flow 208 Acid supply line 209 Product flow to oil/water separation system 210 Aqueous phase discharge line 211 Flow product flow to column 24 212 Discharge line for high boiling materials 213 Product flow to column 25 214 Product flow to column 26 215 Discharge line p for low boiling materials 216 Discharge from bottom of column 217 Pure MMA line 218 Return of low boiling materials
[00136] The examples below serve to further clarify preferred embodiments of the present invention, but are not intended to limit the invention. Example 1
[00137] In a system corresponding to Figure 2, propanal (PA) is continuously reacted with formaldehyde using dimethylamine (DMA) and acetic acid (AcOH). 251 g/h of PA and 349 g/h of a 37 percent formalin solution are homogeneously premixed (1:1 molar ratio). 18.7 g/h of a catalyst solution with 24.8% dimethylamine and 37.9% acetic acid is passed into preheater 12. The two streams are heated to a temperature of 170°C before being combined . The preheated streams are combined in a T-mixer which has direct connection to a tubular reactor (1/16 inch tube, 4.2 m length). The reactor temperature is controlled by an oil bath operated at 180°C, the residence time is 10 s, and the pressure in the tubular reactor is 7000 kPa (70 bar). Downstream of the tubular reactor, the mixture is depressurized at valve 14 and is introduced into column 15. 335 g/h of material discharged at the bottom of the column is returned to reactor 13, and 370 g/h of material discharged at the bottom of the column are passed for disposal in the form of wastewater. After condensation of the upper flow in condenser 16 and phase separation at 17, a methcrolein-rich phase with a methcrolein content of 96.5% is discharged as product 111, and the aqueous material discharged from the phase separator is returned to the column 15. Conversion is 99.9% and yield is 98.1%, based on propionaldehyde. The residual water content of the methacrolein used in Examples 2 to 4 was 1.7% by weight. Example 2
Catalyst 1 (0.9% Au - 1.1% NiO over SiO 2 -Al 2 O 3 -MgO) was produced by analogy with Example 1 of European patent application publication No. EP 2 210 664 A1. A solution of 375 g aluminum nitrate nonahydrate, 256 g magnesium nitrate hexahydrate and 54 g 60% nitric acid in 500 ml water was added dropwise at 15°C to 2 kg of 10 to 20 nm particle size silica sol solution (Nissan Chemical Industries, Snowdex N-30, 30% by weight SiO 2 ). The mixture was stirred at 50°C for 24 hours, then cooled to room temperature, spray dried (130°C) and calcined (300 to 600°C, 10 hours total). 30 g of this SiO2-Al2O3-MgO support were suspended in 100 ml of water and heated to 90°C. After 15 min at 90°C, this suspension was added to a solution of 1.64 g of nickel nitrate hexahydrate and 530 mg of auric acid (HAuCl4) in 100 ml of water. After stirring at 90°C for an additional 30 minutes, the mixture was cooled and the solid removed, then washed three times with 100 ml of fresh water and in each case stirred at 20°C for 5 minutes and removed by filtration. The catalyst was dried at 105°C within a period of 10 hours and calcined at 450°C within a period of 5 hours in air. ICP analysis showed that the resulting violet powder comprised 1.1% Ni and 0.9% Au. The average size of the gold nanoparticles (TEM) was less than 5 nm.
[00139] A mixture of 0.67 g of methcrolein (from Example 1), 5.65 g of methanol and 504 mg of Au 1 catalyst was stirred in an autoclave under 1100 kPa (11 bar) of an O2 gas mixture /N2 (7% by volume O2) at 80°C within a period of 2 hours, then cooled and filtered and analyzed by GC. The MAL conversion was 98.4%, the MMA production was 94.8%, the MMA selectivity was 96.3%, and the space-time production was 9.3 mol MMA/kg cat -H. Example 3
Catalyst 2 (1% Au-5% ZnO-5% MgO over SiO2) was produced by analogy with Example 1-6 of European patent application publication No. EP1393800A1. 89 g of a commercially available SiO2 support (Cariact Q-10, 75-150 µm, Fuji Silisia) was impregnated with a solution of 18.3 g of zinc nitrate hexahydrate and 12.8 g of hexahydrate of magnesium nitrate in 90 ml of water, dried at 120°C within a period of 12 hours, and then calcined at 600°C within a period of 4 hours. 300 ml of a 20 mmol/L solution of HAuCl4 were adjusted with a 0.5 M NaOH solution at 70°C to pH = 7, and the previously produced SiO2-ZnO-MgO support was added at the stated temperature, with agitation. After further stirring at 70°C for one hour, the mixture was cooled and filtered, and the catalyst was washed three times with 400 ml of fresh water, being stirred in each case at 20°C for 5 minutes. After stirring at 100°C for 10 hours, the material was calcined at 400°C within a period of 3 hours in air. ICP analysis showed that the resulting violet powder comprised 1.5% Au. The average size of the gold nanoparticles was less than 5 nm.
[00141] A mixture of 0.60 g of methcrolein (from Example 1), 5.76 g of methanol and 300 mg of catalyst 2 was stirred in an autoclave under 1100 kPa (11 bar) of an O2/N2 gas mixture (7% by volume O2) at 80°C within a 2 hour period, then cooled and filtered and analyzed by GC. The MAL conversion was 85.5%, the MMA production was 83.4%, the MMA selectivity was 97.5%, and the space-time production was 14.0 mol MMA/kg cat -H. Example 4
Catalyst 3 (1.5% Au-5% La2O3-5% MgO over SiO2) was produced by analogy with Example 1-7 of European patent application publication No. EP1393800A1. 88.5 g of a commercially available SiO2 support (Cariact Q-10, 75150μm, Fuji Silisia) was impregnated with a solution of 13.3 g of lanthanum nitrate hexahydrate and 12.8 g of lanthanum nitrate hexahydrate. magnesium nitrate in 90 ml of water, dried at 120°C within a period of 12 hours, and then calcined at 600°C within a period of 4 hours. 450 ml of a 20 mmol/L HAuCl4 solution were adjusted with a 0.5 M NaOH solution at 70°C to pH = 7, and the previously produced SiO2-La2O3 support was added at the stated temperature, with stirring . After further stirring at 70°C for one hour, the mixture was cooled and filtered, and the catalyst was washed three times with 400 ml of fresh water, being stirred in each case at 20°C for 5 minutes. After stirring at 100°C for 10 hours, the material was calcined at 400°C within a period of 3 hours in air. ICP analysis showed that the resulting violet powder comprised 1.5% Au. The average size of the gold nanoparticles was less than 5 nm.
[00143] A 42.9% solution of methacrolein (from Example 1) in methanol was continuously introduced at a flow rate of 420 g/h into a 2.5 L stirred tank reactor mechanically stirred with a separator. catalyst to which 255 g of catalyst 3 had been loaded. A solution of NaOH in methanol (1 to 4% by weight) was added at a flow rate of 40 g/h to maintain the pH of the reaction mixture at about 7. The amount of air continuously introduced into the reactor 500 kPa (5 bar) and 80°C was sufficient in order to provide a residual proportion of oxygen in the exhaust gas of about 4% by volume of O2. The product mixture continuously withdrawn from the system was analyzed by means of GC. 50 h after the start of the method, the metacrolein conversion was 78.5%, the MMA production was 76.5%, the MMA selectivity was 97.4%, and the space-time production was 9 .8 mol MMA/kg cat-h. The reaction mixture obtained in reactor 21 was introduced at level 30 (from above) into distillation column 22 (45 levels, diameter 15 cm, height 6 m). The temperature of the material at the bottom of the column was 84°C, and the top temperature was 31°C. The methcrolein/methanol mixture was withdrawn from the column at level 5 (from above) and returned to reactor 21. The composition withdrawn from the material at the bottom of distillation column 22 at a flow rate of 500 g/h was composed of MMA which also comprised methanol, methacrylic acid, sodium methacrylate and other components. The amount of a 10% aqueous sulfuric acid continuously introduced from a feed vessel into said flow (line 209) was sufficient so as to provide pH = 2 in the resulting mixture. The resulting mixture was separated by means of a centrifuge in the water/oil separation system 23. The organic phase was introduced at level 20 (from above) at a flow rate of 375 g/h into distillation column 24 (30 levels, diameter 10 cm, height 5 m). Said column was operated at 150 mm Hg, the temperature of the material at the bottom of the column being 70°C and the top temperature being 45°C. Raw MMA was taken from the top of column 24 at a flow rate of 288 g/h and was introduced at level 10 (from above) into column 25 (30 levels, diameter 10 cm, height 5 m). Column 25 was operated at 250 mm Hg, the temperature of the material at the bottom of the column being 80°C and the top temperature being 50°C. Purified MMA was withdrawn at a flow rate of 281 g/h from the material at the bottom of column 25 and was introduced at level 35 (from above) within column 26 (70 levels, diameter 10 cm, height 5 m) . Column 26 was operated at 140 mm Hg, the temperature of the material at the bottom of the column being 80°C and the top temperature being 55°C. Pure MMA was withdrawn from the top of column 26 at a flow rate of 250 g/h. The total production of methyl methacrylate isolated from methcrolein was 97.2% after the elaboration described above.Table 1: Summary of reactions for steps A) and B):
Comparative values of prior art:
[00144] The following Comparative Examples (Comparison 5 to 8) compare possible methods and combinations of various methods according to the prior art with the corresponding selectivities of the individual steps and the total methods. Comparative Example 5 Reaction A: Isobutylene ^ Methacrolein Reaction B: Methacrolein Methacrylic acid Reaction C: Methacrylic acid ^ Methyl methacrylate C = conversion S = selectivity Reaction A (eg, United States Patent Application Publication No. US 7012039B2, Example 1, pressure < 200 kPa(2 bar)): S(MAL) = 88.3%, S(MAA) = 2.4% Water addition H2O/MAL = 1.7 (mol/mol) Reaction B, (eg European Patent Application Publication No. EP 0376117B1, Example 1, pressure < 200 kPa (2 bar)) S(MAA) = 89.2% Water addition H2O/MAL = 5.5 (mol/mol) ) Reaction C (eg, United States Patent Application Publication No. US 20020188151A1) S(MMA) ~ 100% Total selectivity of reactions A + B + C = S(MAL+MAA from IBN)*S( MAA from MAL)*S(MMA from MAL) = 80.9% Comparative Example 6: Reaction A: Isobutylene ^ Methacrolein Reaction B: Methacrolein ^ Methyl methacrylate Reaction A (eg publication of US patent application United States No. US 7012039B2, Exe mple 1, pressure < 200 kPa (2 bar)): S(MAL) = 88.3%, S(MAA) = 2.4% Water addition H2O/MAL = 1.7 (mol/mol) Reaction B, variant 1 (United States Patent Application Publication No. US 7012039B2, Example 1): S(MMA) = 90.7% Reaction B, variant 2 (European Patent Application Publication No. EP 2 210 664 A1, Example 7): S (MMA) = 97.2% Total selectivity A + B (variant 1): S(MMA from IBN) = S(MAL)*S(MMA) = 80.1 % Total selectivity A + B (variant 2): S(MMA from IBN) = S(MAL)*S(MMA) = 85.8 % Comparative example 7 Reaction A: Propionaldehyde ^ Methacrolein Reaction B: Methacrolein ^ Methacrylic acid Reaction C: Methacrylic acid ^ Methyl methacrylate Reaction A (eg German Patent Application Publication No. DE 3213681A1, Example 1) S(MAL) = 98.1% Reaction B (eg European Patent Application Publication No. EP 0376117B1, Example 1, pressure < 200 kPa (2 bar)) S(MAA) = 89.2% Water addition MAL/H2O = 5.5 (mol/mol) Reaction C (eg publication of application for Pa US try No. US 20020188151A1) S(MMA) ~ 100 % Total selectivity of steps A + B + C = S(MMA from PA) = S(MAL from PA)*S(MAA from MAL) *S(MMA from MAA) = 87.5% Comparative example 8 Reaction A: Propionaldehyde Methacrolein Reaction B: Methacrolein ^ Methyl methacrylate Reaction A, (CN101074192A1, pressure < 200 kPa (2 bar)) S(MAL) = 95.2 % Reaction B, (CN101074192A1) S(MMA) = 98.2% Total selectivity of steps A + B: S(MMA from PA) = S(MAL)*S(MMA) = 93.5 % Table 2: Comparison of methods (part 1)

[00145] Comparative methods 5 to 7 in particular require large molar amounts of water separately added during the reaction steps, whereas the total selectivities are markedly lower.Table 3: Comparison of methods (part 2)

[00146] As shown in the table above, the reaction according to the invention (Example 4) can be carried out in step A) with catalytic amounts of amine base, based on MAL, whereas comparative example 8 requires an excess catalyst stoichiometry for this purpose. The value of 9.8 for the space-time production of step B) of the claimed method is likewise more than twice as high as in Comparative Example 8.

权利要求:
Claims (16)
[0001]
1. Method for the production of methyl methacrylate comprising the following steps: (A) production of methacrolein from propanal and formaldehyde and (B) reaction of the methcrolein obtained in step (A) in an oxidative esterification reaction in order to provide methyl methacrylate, said method being, characterized by the fact that the two steps (A) and (B) occur in a liquid phase at a pressure of from 200 to 10,000 kPa (2 to 100 bar), and the step (B) is carried out in the presence of a catalyst containing heterogeneous noble metals comprising metals and/or comprising metal oxides, steps (A) and (B) being carried out in a continuous method.
[0002]
2. Method according to claim 1, characterized in that step (A) is carried out in the presence of from 0.1 to 20% in mol of organic base and from 0.1 to 20% in mole of acid, based in each case on propanal.
[0003]
3. Method according to claim 1 or 2, characterized in that step (A) is carried out at a temperature of from 100 to 300°C.
[0004]
4. Method according to any one of claims 1 to 3, characterized in that step (A) is carried out at a pressure of from 500 to 10,000 kPa (5 to 100 bar).
[0005]
5. Method according to any one of claims 1 to 4, characterized in that the heterogeneous oxidation catalyst used in step (B) for the oxidative esterification reaction comprises one or more ultra-finely dispersed metals with an average particle size of < 20 nm selected from the group consisting of gold, palladium, ruthenium, rhodium and silver.
[0006]
6. Method according to any one of claims 1 to 5, characterized in that the heterogeneous oxidation catalyst used in step (B) for the oxidative esterification reaction comprises one or more members of the group consisting of lithium, sodium, potassium , calcium, magnesium, scandium, yttrium, lanthanum and other lanthanides with atomic numbers from 58 to 71, silicon, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, os , cobalt, rhodium, iridium, nickel, palladium, platinum, copper, silver, gold, zinc, cadmium, boron, aluminum, gallium, indium, thallium, germanium, tin, lead, antimony, bismuth, tellurium, these being respectively present in metallic and/or oxidized form.
[0007]
7. Method according to any one of claims 2 to 6, characterized in that the reaction of propanal with formaldehyde in order to provide methacrolein according to step (A) uses a secondary amine as an organic base.
[0008]
8. Method according to any one of claims 2 to 7, characterized in that step (A) uses at least one organic acid.
[0009]
9. Method according to any one of claims 2 to 8, characterized in that the molar ratio of acid to organic base is in the range of 20:1 to 1:20.
[0010]
10. Method according to any one of claims 1 to 9, characterized in that the reaction according to step (A) is carried out with a dwell duration in the range of 0.1 to 300 seconds.
[0011]
11. Method according to any one of claims 1 to 10, characterized in that the reaction according to step (B) is carried out with a pressure in the range of 200 to 5,000 kPa (2 to 50 bar).
[0012]
12. Method according to any one of claims 1 to 11, characterized in that the oxidative esterification reaction according to step (B) is carried out at a temperature in the range of 10 to 200°C.
[0013]
13. Method according to any one of claims 1 to 12, characterized in that the oxidative esterification reaction according to step (B) takes place with a molar ratio of methanol to methcrolein in the range of 1:1 to 50: 1.
[0014]
14. Method according to any one of claims 1 to 13, characterized in that the reactor volume in step (A) is smaller than the reactor volume in step (B) and the proportion of the two reactor volumes is in the range of 1:1000 to 1:100.
[0015]
15. Method according to any one of claims 1 to 14, characterized in that the total amount of water separately added in the two steps (A) and (B) during the conduction of the reaction is less than 100% in mol, based on metacrolein.
[0016]
16. Method according to any one of claims 1 to 15, characterized in that no water is separately added in the two steps (A) and (B) during the conduction of the reaction.

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法律状态:
2019-10-08| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|

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2020-06-02| B25D| Requested change of name of applicant approved|Owner name: ROEHM GMBH (DE) |

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2020-06-23| B25G| Requested change of headquarter approved|Owner name: ROEHM GMBH (DE) |

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2020-08-04| B25G| Requested change of headquarter approved|Owner name: ROEHM GMBH (DE) |

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2021-02-02| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|

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2021-07-06| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

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2021-07-13| B350| Update of information on the portal [chapter 15.35 patent gazette]|

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2021-08-24| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 11/04/2014, OBSERVADAS AS CONDICOES LEGAIS. |

优先权:

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申请号 | 申请日 | 专利标题

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EP13002076.1|2013-04-19|

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EP13002076|2013-04-19|

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PCT/EP2014/057380|WO2014170223A1|2013-04-19|2014-04-11|Method for producing methylmethacrylate|

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