Klein, Jens (Bruchh�user Weg 12, Heidelberg, 69124, DE)
Schunk, Stephan Andreas (Kaiserstrasse 59, Heidelberg, 69115, DE)
Demuth, Dirk (Zum W�rth 32, Walldorf, 69190, DE)
Sundermann, Andreas (Eichendorffstrasse 24, Halle, 06114, DE)
Gallei, Ewald (August-Bebel-Strasse 48, Viernheim, 68519, DE)
Hibst, Hartmut (Branichstrasse 23, Schriesheim, 69198, DE)
Storck, Sebastian (Uhlandstrasse 37a, Mannheim, 68167, DE)
Stichert, Wolfram (Oberer Rainweg 63/2, Heidelberg, 69118, DE)
Klein, Jens (Bruchh�user Weg 12, Heidelberg, 69124, DE)
Schunk, Stephan Andreas (Kaiserstrasse 59, Heidelberg, 69115, DE)
Demuth, Dirk (Zum W�rth 32, Walldorf, 69190, DE)
Sundermann, Andreas (Eichendorffstrasse 24, Halle, 06114, DE)
Gallei, Ewald (August-Bebel-Strasse 48, Viernheim, 68519, DE)
Hibst, Hartmut (Branichstrasse 23, Schriesheim, 69198, DE)
Storck, Sebastian (Uhlandstrasse 37a, Mannheim, 68167, DE)
| 1. | ) Système de conversion d\'énergie dans les véhicules électriques, comprenant une batterie (1) , un convertisseur (2) comprenant un primaire et deux secondaires ou plus, une commutation (3) caractérisée par un branchement (4) de chargement, entre la sortie (10) du 5 convertisseur (2) et la batterie(l) , et l\'enttree (9) du convertisseur (2) et la source (1 1 ) , la commutation (3) étant montée de telle sorte qu\'elle établisse exclusivement la liaison (6) entre la source extérieure d\'énergie (11) et l\'entrée (9) du convertisseur(2), ainsi qu\'entre la sortie ( 10) du convertisseur (2) et la batterie (1), et qu\'elle déconnecte le branchement 10 (5) entre la batterie (1) et l\'entrée (9) du convertisseur (2), ou, . qu\'exclusivement, elle établisse la liaison par le branchement (5) entre la batterie (1 ) et l\'entrée (9) du convertisseur (2), et déconnecte le branchement (6) entre la source extérieure (1 1 ) et l\'entrée (9) du convertisseur (2), et le branchement (4) entre la sortie (10) du 15 convertisseur (2) et la batterie (1). |
| 2. | ) Système selon la revendication \, caractérisé par une commutation commandée de telle sorte qu\'elle établisse, simultanément ou non, les déconnexions et les connexions qu\'elle doit effectuer . |
| 3. | ) Système selon les revendications 1 et 2, caractérisé par un ouSJO plusieurs enroulements primaires ,et plusieurs enroulements secondaires. |
| 4. | ) Système selon les revendications 1 , 2 , et 3 , caractérisé par un secondaire piloté de telle sorte que la tension et/ou la fréquence varie . |
| 5. | ) Système selon les revendications 1 , 2 , 3 , et 4 caractérisé par plusieures entrées (9) réparties à différents points du convertisseur (2),• -£ toutes ces entrées étant obligatoirement situées en amont de tout ou partie du système de découpage situé le plus en aval . |
The use of silver-containing catalysts for reactions of substances with at least one C-C-double bond is discussed in detail in the state of the art.
So, the US 2,279, 470 describes in general the epoxidation of olefins in presence of molecular oxygen at"active silver surface catalysts".
The EP-B 0 326 392 relates inter alia to the selective epoxidation of 1,3-butadiene to vinyl oxirane in presence of a silver-containing catalyst. Thereby, halogenated hydrocarbon is co-fed to the reaction in the ppm-range, the temperature range is restricted to 75 °C-325 °C as well as the olefin conversion is restricted to 0.1- 75 %. The respective US-patents of the patent family (for example US 4, 897, 498,
US 4,950, 773) are restricted to promoted silver catalysts, whereby alkali metal salts act as doping components.
In the US 5,362, 890, a saturated hydrocarbon is used additionally as co-feed. Said patent relates to a process for the manufacture of vinyl oxirane from, for example, 1,3-butadiene, whereby 40-90 mole-% of a paraffinic hydrocarbon is used in the educt feed as co-feed. Here, the range of the reaction temperature is between 175 °C and 230 °C.
In none of the before-mentioned documents a silver-containing catalyst is dis- closed, which was produced by means of controlled conditions, in particular the absence of light and at temperatures below standard room temperature (25 °C).
The object of the present invention was providing a silver-containing catalyst for the reaction of compounds with at least one C-C-double bond, in particular for the reaction of 1,3-buadiene to vinyl oxirane, which is characterized in an increased activity and/or conversion and/or selectivity compared with the state of the art when using similar reaction conditions.
Surprisingly, it was found, that clearly increased conversions, yields, and/or se- lectivities can be achieved, if the silver-containing catalyst is produced in absence of light and/or at temperatures below the room temperature.
The present invention relates to a silver-containing catalyst system, which can be applied for the reaction of substrates with at least one C-C-double bond with at least one oxygen-containing or oxygen-supplying component with formation of at least one epoxide. The silver-containing catalyst according to the invention is characterized in that its activity is significantly increased with respect to the sil- ver-containing catalysts of the state of the art, as consequence of the process for the manufacture of the invention, in which the synthesis of a silver-amine com- plex is carried out in absence of light and at temperatures below the room tem-
perature. Moreover, the present invention relates to the use of the addressed cata- lyst for the reaction of substrates with at least one C-C-double bond with at least one oxygen-containing or oxygen-supplying component with formation of at least one epoxide, in particular the corresponding reaction of 1,3-butadiene to vinyl oxirane.
An educt resp. intermediate, which is of particular importance for the chemical industry, is the vinyl oxirane (VO ; 1,3-epoxybutene). VO is because of its double- functionality (reactive epoxide ring, double bond) an important (reactive) inter- mediate. For example, it can be rearranged to crotonaldehyde by means of a ring- opening isomerization, which, in turn, is an important intermediate in the synthe- sis of vitamin E, for the manufacture of sorbic acid (preservative in the food in- dustry and animal feed industry) as well as for the synthesis of 3-methoxybutanol (lubricant, for example in shock absorbers). Also, the acid-catalyzed ring opening of the epoxide ring to the corresponding diol can be carried out easily.
Without restricting the general validity of the extent of protection scope of the present invention, the invention is exemplified in the following inter alia by means of the epoxidation of 1,3-butadiene to vinyl oxirane by using the silver- containing catalyst according to the invention. The reaction of 1,3-buadiene in the gas phase to vinyl oxirane is carried out according to the following reaction equa- tion: 0 02 Ag-containing catalyst Reaction equation: Partial oxidation of 1,3-butadiene in presence of oxygen and in presence of a silver-containing catalyst system.
But, this does not deny that the catalyst according to the invention can also be applied for other reactions, containing the reaction of at least one C-C-double bond with at least one oxygen-containing and/or oxygen-supplying substance.
Essential terms, which are used in the present invention, shall be defined in the following: An"epoxide"in the meaning of the present compound is any substance, which contains at least one oxygen atom, which has a bond to two vicinal carbon atoms, that means carbon atoms, which are linked by means of a chemical bond, which exceeds the degree of a physical interaction, that means which in particular is linked by means of a chemical (covalent) bond with said vicinal carbon atoms.
The terms"conversion","selectivity"and"yield", which are used within the con- text of the present invention, are to be understood in that manner as defined in Fitzer, Fritz, Emig, Technische Chemie, Springer, Heidelberg, 4. Auflage, 1996.
The term"absence of light", which is used within the context of the present in- vention, defines any condition, in which the access of light, that is of photons in the wavelength range of from 400 nm to 800 nm to the reaction space is reduced or prevented by means of constructive methods or other methods. There are no restrictions with respect to said methods.
The term"below reaction temperature", which is used in the context of the present invention, defines any temperature, which is significantly below 25 °C in a man- ner that the reaction proceeds measurably different, for example slower, than said reaction would do at room temperature. In particular, the course of the side reac- tion of the reduction of silver ions to metallic silver is to be suppressed as far as possible.
Now, in the following, the invention shall be described in detail as well as pre- ferred embodiments shall be specified.
There are no restrictions with respect to the manufacture of the catalysts, which are exemplified in the embodiments, apart from that the catalytic active material must contain at least silver according to the process for the manufacture, as well as that during the process for the manufacture at least partially absence of light and/or the existence of a temperature below room temperature is ensured.
Thereby, the silver can be supplied alone or in combination with at least one fur- ther element. Furthermore, it is preferred that the silver is applied at least partially onto at least one support. Thereby, the silver can be in metallic form, oxidic form, mixed-bonded form, as complexed ion, as reduced species as well as in a stoichi- ometric or in a non-stoichiometric composition.
Thereby, in a preferred embodiment, the silver is in complexed form. As com- plexing agent all substances can be used, the one skilled in the art knows from that said substances form with silver at least partially a coordination compound.
Thereby, amines, diamines, alcohols, alkanediols, EDTA, functionalized carbox- ylic acid and carboxylic diacids are preferred. In particular, ethylenediamine is preferred. What is disclosed as aforesaid, preferably relates to all phases before the calcination.
In another preferred embodiment, the silver is in reduced form. As reducing agent, any substance, which is known to the one skilled in the art, can be applied in the synthesis of the active mass, which reduces at least partially the oxidation number of the silver in the respective condition on hand. It is preferred applying an alkane, an alcohol, an amine or another organic molecule, which by means of its redox potential is capable converting the material into a catalytic active and/or selective form. Thereby, the use of ethanolamine is in particular preferred.
In a particular preferred embodiment, the silver is both in reduced form and in complexed form. For example, such a process can be as follows: oxalic acid and ethylenediamine are charged. To it, silver oxide is added, which is dissolved in water. Ethanolamine is added to this mixture. Numerical values are specified in the embodiments. Now, said solution can be applied onto a support.
The active, silver-containing mass can be applied onto a support in any form, can brought into contact with a support or a support can be impregnated with said mass. Thereby, the silver resp. the silver-containing mass can be brought into contact with the support material out from the gas phase or from the liquid phase or as powder or in any combination of the before-mentioned processes.
The bringing into contact can consist of at least one of the processes of the group given below, however, without being restricted to said group: soaking, dunking, impregnating, deposition from the gas phase, mixing, grinding, sputtering, elec- trochemical deposition, chemical deposition without current, vacuum deposition, spreading of a paste-like mass, powder deposition, precipitation from or in a solu- tion, spray drying. In particular, the application by means of bringing into contact of the support material with an aqueous phase is preferred.
In principle, as support material for the silver resp. the silver-containing mass all materials can be applied, which can be brought into contact with silver resp. the silver-containing mass. In a preferred embodiment, the at least one support mate- rial consists of at least one component selected from the following group: sili- cates, in particular Si02 ; alumina oxides, in particular oc-A1203, y-A1203 ; layer silicates, in particular steatite; oxides of the metals of the Main and Auxiliary Groups and, thereby, in particular Ti02, ZrO2 ; cerium oxide (oxides), mixed ox- ides, mixed oxides or oxides, in which parts of the lattice sites of a pure oxide, for example of a silicate, are replaced by at least one further element, and, thereby, in particular zeolites; carbon-containing supports and, thereby, in particular graphite and/or activated carbon, carbides; nitrides, as well as mixtures of at least two of
the before-mentioned support materials. In the meaning of the present invention, Al203-containig supports are in particular preferred.
In the meaning of the present invention, the content of Ag with respect to the sup- port material and expressed in weight-% ranges from 0.01 % up to 10 %. Thereby, in particular, a weight proportion of from 0.1 % to 2.5 % is preferred. Said weight proportion relates to the support steatite and is limited by a possible water absorp- tion, which should not be incorporated in the above-mentioned numerical values.
The silver can form the catalyst as sole component or together with the support, or it is possible adding additional elements to the silver. Said additional elements can be elements from the Groups 1 to 17 of the Periodic Table of the Elements, and can preferably be selected from the Groups 1 to 12 and the Group 17. In particular preferred are the elements K, Rb, Cs, Sr and Ba. There is no restriction with re- spect to the number of additional elements and/or the proportion thereof.
In principle, in the present invention, the catalyst can be available as unsupported active mass (that means as full catalyst), or the catalyst can be available on one of the above-mentioned support materials (that means as shell catalyst, in case the support is not predominantly porous, or as support catalyst in case the support is predominantly porous).
In principle, the calcination of the catalyst, for example after the application of the silver resp. the silver-containing mass, and optional of an additional component and/or after a drying step, can take place at any temperature, which results among normal operating conditions in an economical tolerable durability of the catalyst for the catalytic application according to the invention. It is preferred applying to the calcination step temperatures between 200 °C and 800 °C, and, temperatures of from 200 °C to 500 °C are in particular preferred, and further, temperatures of from 200 °C to below 300 °C are preferred.
The calcination can take place either in air or in a controlled atmosphere. Con- trolled atmospheres in the meaning of the present invention are: inert gases, re- ducing atmospheres, for example inert gases containing hydrogen, water steam, CO, CO2, oxidizing atmospheres, reactive gases, atmospheres with increased or decreased pressure, in particular vacuum, as well as all possible combinations and/or mixtures of the before-mentioned atmospheres.
After the calcination, at least one step of the after-treatment can take place, whereby for the after-treatment in principle any step can be applied the one skilled in the art would apply for the after-treatment of catalysts in general.
In particular, the process for the manufacture of the catalyst according to the in- vention is characterized in that it is carried out in absence of light (as defined above) and/or at temperatures, which are diminished with respect to the room temperature (as likewise defined above). Said conditions must be fulfilled for at least one step of the manufacture of the catalyst, the calcination included. In a preferred embodiment, said condition or said conditions are fulfilled for all steps of the manufacture of the material according to the invention, the calcination be- ing included.
Overall, the process for the manufacture of the silver-containing catalysts contains at least one of the two following steps: (I) reaction of a silver-containing component with at least one complexing agent, (II) reaction of a silver-containing component with at least one reducing agent, wherein at least one of the steps is carried out at least partially in absence of light or at temperatures below the room temperature or in absence of light and at tem- peratures below the room temperature.
Optionally, the process can contain at least one further of the following steps: bringing into contact of the silver-containing component from (I) and/or (II) with a support, (IV) calcination of the support from (III), which was brought into contact, wherein also here one or both of said steps can be carried out optionally in ab- sence of light or at temperatures below the room temperature, or in absence of light and at temperatures below the room temperature.
There are no restrictions with respect to the compounds, which have at least one C-C-double bond, and which are to be reacted using the silver-containing catalyst according to the invention. Thereby, it is preferred, using n-butene, like 1-butene and/or 2-butene (cis/trans). Thereby, the use of 1,3-butadiene is in particular pre- ferred.
In principle, in the meaning of the present invention, there are no restrictions with respect to the oxygen-containing or oxygen-supplying components or substances, which are to be applied for the reaction with at least one compound, which con- tains at least one C-C-double bond. Thereby, oxygen, gases, which contain oxy- gen, in particular air, as well as water, aqueous mixtures, water steam, mixtures containing hydroperoxides in fluidic condition or any mixtures of at least two of the afore-mentioned substances are preferred. Furthermore, it is preferred that the oxygen-containing or oxygen-supplying components are predominantly in gase- ous form, in particular if the reaction is to be carried out in a fixed bed.
In a preferred application, alkenes, preferably alkadienes, further preferred 1,3- butadiene are reacted in presence of oxygen or an oxygen-containing component of an educt gas to the corresponding epoxides, whereby the formation of vinyl oxirane from 1,3-butadiene is preferred, in the presence of the catalyst according to the invention, respectively.
In a preferred embodiment, the process for the reaction of the above-described educts in the gas phase in presence of one of the above-described catalysts with the target of the manufacture of epoxides, is carried out in at least one fixed bed reactor, which is charged with at least one of the silver-containing catalysts of the invention, whereby a tubular reactor with fixed bed is in particular preferred. By using the catalyst according to the invention, it is preferred using as reaction tem- perature according to the reaction of the invention a temperature between 225 °C and 350 °C. For the space rate of the gas (GHSV) values of from 100 to 25.000 h~l are preferred, further preferred of from 2.000 to 20.000 h-1. In the embodiments, conversion, selectivity and yield are shown for different temperatures and values of the GHSV.
The embodiments of the following should exemplify the present invention as well as their technical advantages. No restriction of the disclosure of the general de- scription can be derived from the examples.
Example 1: Reaction of butadiene to vinyl oxirane by using a silver-containing catalyst T3131 (Comparison Example) : For the silver-containing catalyst system T3131, the synthesis of the silver-amine complex is carried out at room temperature and at daylight. Thereby, nitrates in aqueous solution are applied. For the synthesis of the silver-amine complex, 6.3 g oxalic acid, 6 g ethylenediamine and 11.6 g Ag20 are dissolved in 25 ml H20 and 1.7 g ethanolamine are added. A1203-beads from Ceramtec (granulate, diameter approximately 1 mm) are the support. In the present case, the silver load is 2.5 weight-% Ag on the support. Subsequently, the material is temperature-treated for 2 hours at 290 °C in the oven; thereby, the material is overflowed with 6 1/min air.
In Table 1, exemplary results are given for the reaction of butadiene to vinyl oxi- rane (VO) by using the catalyst T3131. For this, for example 1 ml of the material (the catalyst volume is explicitly indicated in the tables) is inserted into a high-
grade steel tubular reactor with an inner diameter of 8 mm (is inert among the reaction conditions, no activity with respect to the target reaction), and is heated from the outside up to the reaction temperature. The analysis of the product gas is carried out by means of a coupling of a micro-GC for the separation of the low boilers (butadiene) with a GC/MS with a Hewlett Packard HP-5 column for the separation and detection of the oxygenates.
Table 1: Catalyst number. mounting volume temperature [°C] GHSV [h 1] convers. sel. to VO yield VO T 3131 2. 0ml 180 12000 2.49 7.15 0.18 T 3131 1.0 mL 180 12000 0.25 58.38 0.15 T 3131 1 ml/1 ml corundum 180 12000 0.00 0.00 0.00 T 3131 1ml/1ml corundum 180 6000 2.65 45.19 1.20 T 3131 1.0 mL 180 6000 3.33 5.73 0.19 T 3131 2. Oml 180 6000 1.96 0.00 0.00 T 3131 1ml/1ml corundum 200 12000 3.72 100. 00 3.72 T 3131 1.0 mL 200 12000 0.00 0.00 0.00 T 3131 2. 0ml 200 12000 0.00 0.00 0.00 T 3131 1ml/1ml corundum 200 6000 6.37 100.00 6.37 T 3131 2. 0ml 200 6000 0.35 100.00 0.35 T 3131 1.0 mL 200 6000 0.00 0.00 0.00 T3131 lmU/1ml corundum 200 3000 5.81 100.00 5.81 T 3131 1.0 mL 200 3000 1.34 79.55 1.07 T 3131 2. Oml 200 3000 3.46 6.34 0. 22 T3131 1ml/1ml corundum 220 12000 1.91 100.00 1.91 T3131 1.0 mL 220 12000 1.84 29.58 0.54 T 3131 2. Oml 220 12000 0.48 0.00 0.00 T 3131 1 ml/1 ml corundum 220 6000 11.51 100.00 11.51 T 3131 2. 0ml 220 6000 2.09 67.08 1.40 T 3131 1.0 mL 220 6000 0.74 100.00 0.74 T 3131 1 ml/1 ml corundum 220 3000 23.85 100. 00 23.85 T 3131 1.0 mL 220 3000 4.20 97.57 4.09 T 3131 2. 0ml 220 3000 4.16 41.65 1.73 T3131 1ml/1ml conundum 240 12000 13.29 100.00 13.29 T 3131 1. 0 mL 240 12000 4.91 99.04 4.86 T 3131 2. Oml 240 12000 5.65 82.20 4.64 T 3131 1ml/1ml corundum 240 6000 22.26 100.00 22.26 T 3131 2. 0ml 240 6000 5.35 100.00 5.35 T 3131 1.0 mL 240 6000 3.80 100.00 3.80 T 3131 1 ml/1 ml corundum 240 3000 32.13 100.00 32.13 T3131 1.0 mL 240 3000 8.40 100.00 8.40 T 3131 2. 0ml 240 3000 4.78 100.00 4.78 T3131 1ml/1ml conundum 260 12000 32.53 100.00 32.53 T 3131 1.0 mL 260 12000 19.17 100.00 19.17 T3131 2. 0ml 260 12000 21.14 80.53 17.02 T 3131 1 mlli ml corundum 260 6000 40.64 91.95 37.37 T 3131 2. Oml 260 6000 13.30 96.49 12.83 T3131 1. 0 mL 260 6000 11. 12 100. 00 11. 12 T 3131 1. 0 mL 260 3000 23.46 70.50 16.54 T 3131 1ml/1ml corundum 260 3000 68.38 16.84 11.52 T 3131 2. Oml 260 3000 18.10 42.84 7.76 T 3131 1. 0 mL 280 12000 46.19 53.75 24.83 T 3131 2. 0ml 280 12000 56.48 26.40 14.91 T 3131 1ml/1ml corundum 280 12000 79.47 7.83 6.23 T 3131 1. 0 mL 280 6000 30.49 67.81 20.68 T 3131 2. Oml 280 6000 36.32 30.23 10.98 T 3131 1ml/1ml corundum 280 6000 88.05 0.00 0.00 T 3131 1. 0 mL 280 3000 62.69 9.88 6.19 T 3131 1ml/1ml corundum 280 3000 89.55 0.00 0.00 T3131 2. Oml 280 3000 95.38 0.00 0.00 T3131 1. 0 mL 300 12000 93. 61 0.00 0.00 T 3131 1ml/1ml corundum 300 12000 88.26 0.00 0.00 T 3131 2. 0ml 300 12000 100.00 0.00 0.00 T 3131 1. 0 mL 300 6000 92.52 0.00 0.00 T 3131 1ml/1ml corundum 300 6000 87.39 0.00 0.00 T 3131 2. Oml 300 6000 100.00 0.00 0.00 T 3131 1. 0 mL 320 12000 93.85 0.00 0.00 T3131 1ml/1ml conundum 320 12000 89.07 0.00 0.00 T3131 2. Oml 320 12000 100.00 0.00 0.00
Example 2: Reaction of butadiene to vinyl oxirane by using the silver-containing catalyst T3326 of the invention For the silver-containing catalyst system T3326, the synthesis is carried out analogously to Example 1. The only differences are that here the synthesis is car- ried out in darkness and by means of cooling with an ice bath (0 °C). Furthermore, 0.001 weight-% Cs are added in form of CsNO3 as doping component. Exemplary results are indicated in Table 2 for the reaction of butadiene to vinyl oxirane (VO) by using the catalyst T3326.
Compared with the catalyst from Example 1, which was not subjected to the proc- ess for the manufacture according to the invention, it can clearly be realized that yields can be achieved with respect to the vinyl oxirane, which are better up to a factor 3 (with the same or improved selectivity). In particular, this applies in the meaning that yield, conversion and selectivity are improved over the complete breadth of the conditions, that means that yield, conversion and selectivity are improved systematically. Thus, the technical advantage of the silver-containing catalyst according to the invention can clearly be realized for the one skilled in the art.
Table 2: catalyst number mounting volume temperature [°C] GHSV [h-1] convers. sel. to VO yield VO T 3326 2. 0ml 180 12000 15.49 100.00 15.49 T 3326 1ml/1mt corundum 180 12000 10.11 100.00 10.11 T 3326 1.0 mL 180 12000 7.87 100.00 7.87 T 3326 2. 0ml 180 6000 22. 95 100.00 22.95 T 3326 1 ml/l ml corundum 180 6000 20.24 100.00 20.24 T 3326 1.0 mL 180 6000 15.60 100.00 15.60 T 3326 2. 0ml 200 12000 36.48 100.00 36.48 T 3326 1ml/1ml corundum 200 12000 26.59 100.00 26.59 T 3326 1. 0 rriL 200 12000 20.84 100.00 20.84 T 3326 2. 0ml 200 6000 46.15 100.00 46.15 T 3326 1ml/1ml corundum 200 6000 38.78 100.00 38.78 T 3326 1.0 mL 200 6000 32.09 100.00 32.09 T 3326 2. 0ml 200 3000 63.69 100.00 63.69 T 3326 1 mlll ml corundum 200 3000 50.20 100.00 50.20 T 3326 1.0 mL 200 3000 49.71 100.00 49.71 T 3326 2. 0ml 220 12000 56.54 100.00 56.54 T 3326 1 ml/1 ml corundum 220 12000 43.54 100.00 43.54 T 3326 1.0 mL 220 12000 43.01 100.00 43.01 T 3326 2. 0ml 220 6000 67.48 100.00 67.48 T 3326 1 ml/1 ml corundum 220 6000 56.93 100.00 56.93 T 3326 1.0 mL 220 6000 54. 81 100.00 54.81 T 3326 2. 0ml 220 3000 83.25 100.00 83.25 T 3326 1.0 mL 220 3000 74.78 100.00 74.78 T 3326 1 ml/1 ml corundum 220 3000 71.19 100.00 71.19 T 3326 2. 0ml 240 12000 82.33 100.00 82.33 T 3326 1.0 mL 240 12000 66.61 100.00 66.61 T 3326 1ml/1ml corundum 240 12000 61.88 100.00 61.88 T 3326 2. Oml 240 6000 81.26 100.00 81.26 T 3326 1.0 mL 240 6000 72. 71 100. 00 72. 71 T 3326 1mU/1ml corundum 240 6000 69.91 100.00 69.91 T 3326 1.0 mL 240 3000 86.89 100.00 86.89 T 3326 2. 0ml 240 3000 89.99 81.80 73.62 T 3326 1ml/1ml corundum 240 3000 79.50 77.05 61.25 T 3326 2. 0ml 260 12000 89.95 84.07 75.62 T 3326 1 mlll ml corundum 260 12000 70.99 100.00 70.99 T 3326 1.0 mL 260 12000 97.12 10.39 10.09 T 3326 1.0 mL 260 6000 86.65 100.00 86.65 T 3326 2. 0ml 260 6000 90.62 75.77 68.66 T 3326 1 ml/1 ml corundum 260 6000 77.06 87.20 67.20 T 3326 1.0 mL 260 3000 95.49 41. 38 39.51 T 3326 1ml/1ml corundum 260 3000 82.87 27.89 23.11 T 3326 2. 0ml 260 3000 93.21 12.76 11.89 T 3326 1ml/1ml corundum 280 12000 76.05 60.61 46.10 T 3326 2. 0ml 280 12000 100.00 4.66 4.66 T 3326 1.0 mL 280 12000 100.00 2.23 2.23 T3326 1ml/1micorundum 280 6000 81.11 37.78 30.64 T 3326 1.0 mL 280 6000 95.32 12.47 11.89 T 3326 2. 0ml 280 6000 95.17 1.63 1.55 T 3326 1ml/1ml corundum 280 3000 85.00 3.33 2.83 T 3326 1.0 mL 280 3000 100.00 1.35 1.35 T 3326 2. Oml 280 3000 91.35 0.00 0.00 T 3326 1 ml/1 ml corundum 300 12000 79.43 28.68 22.78 T 3326 2. 0ml 300 12000 100.00 0.86 0.86 T 3326 1.0 mL 300 12000 100.00 0.57 0.57 T 3326 1ml/1ml corundum 300 6000 85.26 9.40 8.01 T 3326 1.0 mL 300 6000 100.00 0.98 0.98 T 3326 2. Oml 300 6000 100.00 0.00 0.00 T 3326 1 ml/1 ml corundum 320 12000 80.88 11.72 9.48 T 3326 1.0 mL 320 12000 100.00 0.26 0.26 T 3326 2. 0ml 320 12000 100.00 0.16 0.16
Example 3: Reaction of butadiene to vinyl oxirane by using the silver-containing catalyst T3327 according to the invention: The synthesis of the silver-containing catalyst system T3327 is carried out analo- gously to Example 1. The only differences to Example 1 are here the lead-through of the synthesis in darkness and by means of cooling with an ice bath (0 °C).
Here, in difference to Example 2, an undoped Ag-catalyst is used. Exemplary re- sults are indicated in Table 3 for the reaction of butadiene to vinyl oxirane (VO) by using the catalyst T3327. Thereby, the conversions, selectivities and yields are not as good as in Example 2, but better than in Example 1.
Table 3: catalyst number mounting volume temperature [°C] GHSV [h-1] convers. sel. to VO yield VO T 3327 2. Oml 180 12000 1.20 49.43 0.59 T3327 1m !/1m ! corundum 180 12000 0.53 100.00 0.53 T 3327 1.0 mL 180 12000 0. 55 65.28 0.36 T 3327 1 ml/1 ml corundum 200 12000 3.85 100.00 3.85 T 3327 2. Oml 200 12000 0.55 100.00 0.55 T 3327 1.0 mL 200 12000 0.00 0.00 0.00 T 3327 1ml/1ml corundum 220 12000 4.35 77.36 3.36 T 3327 1.0 mL 220 12000 3.31 46.58 1.54 T 3327 2. Oml 220 12000 2.71 55.34 1.50 T 3327 1ml/1ml corundum 240 12000 16.77 100.00 16.77 T 3327 2. Oml 240 12000 13.45 100.00 13.45 T 3327 1.0 mL 240 12000 9.88 100.00 9.88 T 3327 1ml/lml corundum 260 12000 40.09 94.49 37.88 T 3327 1.0 mL 260 12000 36.40 100.00 36.40 T 3327 2. 0ml 260 12000 62.01 54.96 34.08 T 3327 2. Oml 280 12000 100.00 0.00 0.00 T3327 1.0 mL 280 12000 98.31 0.00 0.00 T 3327 1 mUi ml corundum 280 12000 84.68 0.00 0. 00 T 3327 2. Oml 300 12000 100.00 0.00 0.00 T 3327 1.0 mL 300 12000 100.00 0.00 0.00 T 3327 1 ml/1 ml corundum 300 12000 86.03 0.00 0. 00 T 3327 2. Oml 320 12000 100.00 0.00 0.00 T 3327 1.0 mL 320 12000 100.00 0.00 0.00 T 3327 1ml/1ml corundum 320 12000 83.26 0.00 0. 00
Example 4: Reaction of butadiene to vinyl oxirane by using the silver-containing catalyst T3321 according to the invention The synthesis for the silver-containing catalyst system T3321 is carried out analo- gously to Example 2, however at room temperature. Exemplary results are indi- cated in Table 4 for the reaction of butadiene to vinyl oxirane (VO) by using the catalyst T3321. Here, too, conversions, selectivities and yields are clearly better than in Example 1 (Comparison Example), which represents the state of the art.
Therewith, it is shown that already the absence of light leads to an essential im- provement of the catalyst properties.
Table 4: catalyst number mounting volume temperature [°C] GHSV [h 1] convers. sel. to VO yield VO T 3321 2. 0ml 180 12000 15.28 100.00 15.28 T 3321 1.0 mL 180 12000 8.70 100.00 8.70 T 3321 1ml/1ml corundum 180 12000 6.82 100.00 6.82 T 3321 2. 0ml 180 6000 18.31 100.00 18.31 T 3321 1.0 mL 180 6000 15.37 100.00 15.37 T 3321 1 ml/1 ml corundum 180 6000 14.88 100.00 14.88 T 3321 2. 0ml 200 12000 30.23 100.00 30.23 T 3321 1.0 mL 200 12000 21.63 100.00 21.63 T 3321 1 mlii ml corundum 200 12000 19.87 100.00 19.87 T 3321 2. 0ml 200 6000 41.04 100.00 41.04 T 3321 1.0 mL 200 6000 30.64 100.00 30.64 T 3321 1 mU1 ml corundum 200 6000 30.46 100.00 30.46 T 3321 2. 0ml 200 3000 63.38 100.00 63.38 T 3321 1.0 mL 200 3000 50.29 100.00 50.29 T 3321 1 ml/1 ml corundum 200 3000 38.76 100.00 38.76 T 3321 2. 0ml 220 12000 37.71 100.00 37.71 T3321 1ml/1micorundum 220 12000 36.65 100.00 36.65 T 3321 1.0 mL 220 12000 33.22 100.00 33.22 T 3321 2. 0ml 220 6000 67.10 100.00 67.10 T 3321 1.0 mL 220 6000 54.69 100.00 54.69 T 3321 1ml/1ml corundum 220 6000 44.74 100.00 44.74 T 3321 2. 0ml 220 3000 84.33 100.00 84.33 T 3321 1.0 mL 220 3000 72.58 100.00 72.58 T 3321 1 ml/1 ml corundum 220 3000 55.90 100.00 55.90 T 3321 2. 0ml 240 12000 81.72 100.00 81.72 T 3321 1.0 mL 240 12000 63.68 100.00 63.68 T 3321 1ml/1ml corundum 240 12000 58.98 100.00 58.98 T 3321 2. 0ml 240 6000 84.27 100.00 84.27 T 3321 1.0 mL 240 6000 72.67 100.00 72.67 T 3321 1 ml/1 ml corundum 240 6000 58.97 100.00 58.97 T 3321 1.0 mL 240 3000 86.85 90.60 78.68 T 3321 1ml/1ml corundum 240 3000 68.43 74.38 50.89 T 3321 2. 0ml 240 3000 95.59 50.79 48.55 T 3321 1.0 mL 260 12000 78.43 100.00 78.43 T 3321 2. 0ml 260 12000 93.19 72.63 67.68 T 3321 1 mill ml corundum 260 12000 68.09 89.97 61.26 T 3321 1.0 mL 260 6000 85.72 89.77 76.96 T 3321 1ml/tml corundum 260 6000 67.56 85.79 57.96 T 3321 2. 0ml 260 6000 94.43 60.67 57.30 T 3321 1ml/1ml corundum 260 3000 74.19 29.00 21. 51 T 3321 1.0 mL 260 3000 93.90 21.16 19.87 T 3321 2. 0ml 260 3000 100.00 3.77 3.77 T 3321 1ml/1ml corundum 280 12000 73.59 43.89 32.30 T 3321 1.0 mL 280 12000 94.18 24.19 22.78 T 3321 2. 0ml 280 12000 100.00 10.12 10.12 T 3321 1ml/1ml corundum 280 6000 72. 50 38.33 27.79 T 3321 1.0 mL 280 6000 91.96 9.99 9.19 T 3321 2. Oml 280 6000 100.00 4.56 4. 56 T 3321 1ml/1ml corundum 280 3000 76.78 4.34 3.33 T 3321 1.0 mL 280 3000 93.99 0.41 0.38 T 3321 2. Oml 280 3000 100.00 0.00 0.00 T 3321 1ml/1ml corundum 300 12000 75.53 25.26 19.08 T 3321 1.0 mL 300 12000 96.11 5.24 5.03 T 3321 2. 0ml 300 12000 100.00 1.12 1.12 T 3321 1ml/1ml corundum 300 6000 73.66 10.66 7.85 T 3321 1.0 mL 300 6000 93.20 0.50 0.46 T 3321 2. 0ml 300 6000 100.00 0.12 0.12 T 3321 1ml/1ml corundum 320 12000 76.41 10.27 7.85 T 3321 1.0 mL 320 12000 96.45 1.67 1.61 T 3321 2. 0ml 320 12000 100.00 0.24 0.24
Example 5: Reaction of butadiene to vinyl oxirane by using a silver-containing catalyst T2502 (lower silver content ; Comparison Example) : For the manufacture of the silver-containing catalyst system T2502, the synthesis of the silver-amine complex was carried out at room temperature and at daylight.
Thereby, the nitrates are applied in aqueous solution. For the synthesis of the sil- ver-amine complex 2.52 g oxalic acid, 2.4 g ethylenediamine and 4.635 g Ag20 are dissolved in 10 ml H2O, and 1.36 g ethanolamine are added. A1203-beads from Ceramtec are the support. In the present case, the load with silver is 0.5 weight-% Ag on the support. Subsequently, the material is temperature-treated for 3 hours at 290 °C in the oven; thereby, the material is overflowed with 6 1/min air. In Table 5, exemplary results are summarized for the reaction of butadiene to vinyl oxirane by using the catalyst T2502. The testing takes place analogously to Example 1.
Table 5: catalyst number mounting volume temperature [oc] GHSV th ~1] convers. sel. to VO yield VO T 2502 1.0 mL 220 12000 0.00 0.00 0.00 T 2502 1.0 mL 240 12000 2.86 38.09 1.09 T2502 1.0 mL 260 12000 9.60 100.00 9.60 T 2502 1.0 mL 280 12000 26.77 100.00 26.77 T 2502 1. 0 mL 300 12000 63.48 55.53 35. 25 T2502 1.0 mL 320 12000 100.00 0.15 0.15 T 2502 1.0 mL 340 12000 100.00 0.00 0.00 T 2502 1.0 mL 340 12000 100.00 0.00 0.00 T 2502 1.0 mL 360 12000 100.00 0.00 0.00 T 2502 1.0 mL 380 12000 100.00 0.00 0.00
Example 6: Reaction of butadiene to vinyloxiran by using a silver-containing catalyst T2530 (Comparison Example) : For the synthesis of the silver-containing catalyst system T2530, the synthesis of the silver-amine complex was carried out at room temperature and at daylight.
Thereby, the nitrates are applied in aqueous solution. For the synthesis of the Ag- amine complex 2.52 g oxalic acid, 1.2 g ethylenediamine and 4.635 g Ag20 are dissolved in 10 ml H20 and 0.68 g ethanolamine are added. A1203-beads from Ceramtec are the support. In the present case, the silver load is 1.0 weight-% Ag on the support. Subsequently, the material is temperature-treated for 3 hours at 290 °C in the oven. Thereby, the material is overflowed with 6 1/min air. In Table 6, the exemplary results are summarized for the reaction of butadiene to vinyl oxirane by using the catalyst T2530. The testing is carried out analogously to Ex- ample 1. It is shown here, as in the last Example, that conversions, selectivities and yields are achieved, which are in total clearly lower, if the growth of the silver crystals is not controlled by means of avoiding exposing and by means of cooling.
Table 6: catalyst number mounting space temperature [°C] GHSV [h\'] se). to VO yield VO T 2530 1.0 mL 220 12000 0.00 0.00 0.00 T 2530 1.0 mL 240 12000 7.24 100.00 7.24 T 2530 1.0 mL 260 12000 24.91 100.00 24.91 T 2530 1.0 mL 280 12000 41.57 100.00 41.57 T 2530 1.0 mL 300 12000 80.36 38.86 31.23 T2530 1.0 mL 320 12000 100.00 0.14 0.14 T 2530 1.0 mL 340 12000 100. 00 0.00 0.00 T 2530 1.0 mL 340 12000 100.00 0.00 0.00 T 2530 1.0 mL 360 12000 100.00 0.00 0.00 T 2530 1.0 mL 380 12000 100.00 0.00 0.00