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    • 专利摘要:
    1. METHOD OF OBTAINING ACETIC ACID, ETHANOL, ACETALDEHYDE AND THEIR DERIVATIVES by the interaction of carbon monoxide with hydrogen in the presence of rhodium-containing, supported catalyst at a temperature of 200350 C and a pressure of 20-200 atm, characterized in that, p. goal of selectivity; In the process, a rhodium-magnesium-halogen complex compound, or rhodium and magnesium halides, or, are used as a rhodium-containing catalyst. rhodium halide and magnesium halide, an alkaline complex compound, or rhodium geshogenide, and silicate, or acetyl acetonate, or magnesium aluminate, or rhodium and magnesium nitrate and hydrogen halide, calcium chloride or tin, or chromium, or dimeric rhodium dicarbonyl chloride and magnesium acetate or magnesium acetate, or dimeric rhodium dicarbonyl chloride and calcium acetate or magnesium acetate, or dimeric rhodium dicarbonyl chloride and magnesium acetate or magnesium acetate, or tin, chromium, or dimeric equal to 1 and / or 2 in all compounds. 2. A method according to claim 1, characterized in that the process uses a catalyst obtained by reducing the compounds of trivalent rhodium at 225-275 ° C to compounds of rhodium with a valence of 1 and / or 2., 3. Method by Clause 1, of which it is necessary that salt or the compound of magnesium is continuously or periodically combined with the original components in the process. 4. The method according to claim 1, that is, and with the fact that a hydrogen halide or organic halogen-containing compound is fed continuously or periodically together with the starting components into the process. VIEVA process hydrogen halide. ffi cx. Priority on points: 04/04/78 under item 1 06/10/78 under item 2 11/18/78 under item 3 a. Nt
    公开号:SU1064864A3
    申请号:SU792745953
    申请日:1979-04-03
    公开日:1983-12-30
    发明作者:Шмидт Ханс-Йоахим；Вундер Фридрих；Арпе Ханс-Юрген；Инго Лойпольд Эрнст
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to an improved process for the production of acetic acid, ethanol, acetaldehyde and their derivatives, which are used to obtain resins, science, the known method of producing acetic acid, ethanol, acetaldehyde, and derivatives by reacting carbon monoxide with hydrogen in the presence of a catalyst containing rhodium metal. , on: carrier at 150–50 ° С and pressure 1.05–700 atm. Productivity of the process is 250-275 m / h. The selectivity of the process for C-products there on converted carbon monoxide 40, s%: tii. The disadvantages of this method are low selectivity and productivity of the process. The closest to the proposed method is the production of acetic acid, ethanol, acetaldehyde and their derivatives by reacting carbon monoxide with hydrogen in the presence of a catalyst containing metallic rhodium and manganese, at 150-450s and pressure 20 -200 atm The productivity of the process is 240432 g / l h, the selectivity of the process is 60% pJ. The disadvantage of this method is the low selectivity of the process. The purpose of the invention is to increase the selectivity of the process. The goal is achieved by the fact that, according to the method of obtaining uksunuy acid, ethanol, acetaldehyde and their derivatives by the interaction of carbon monoxide with hydrogen in the presence of a rhodium-containing catalyst on a carrier at 200-350 s and a pressure of 20-200 atm, the rhodium-containing catalyst is used Rhodium | 1gnium-halogen-complex compound, or rhodium and magnesium halides, | Shi rhodium halide and magnesium-halogen | shepherd complex, rhodium halide and silicate, or acetylacetonate, or magnesium aluminate or rhodium and nitrate hydrogen and halogen, or calcium chloride or tin, or chromium, or dimeric rhodium dicarbonyl chloride and magnesium acetate, and the valence of rhodium in all compounds is 1 and / or 2. The process uses a catalyst obtained by reducing compounds of trivalent rhodium at H25- 275c before the rhodium compound with a valence of 1 and / or 2. Continuously or periodically with the initial components, feed the salt or magnesium compound with a hydrogen halide or organic halide-containing compound, giving the conditions of the halo gene hydrogen d ,. Chloride or bromide and / or roodi iodide are used as rhodium salts, as well as double salts with halogen | alkali metal nida, for example, such as dipotassium trichloride, and rhodium, tris-triphenylphosphine, chloride, bromide or rhodium iodide as salts. (1), tyr-tris-tri (., Phenyl-phosphine-rhodium (III) -chloride, dichloro-bis-ethylenediamine-rhodium) (1) tris-ethylenediamine-rhodium chloride {111 / chloride, bis-three-o- tolylphosphine-rhodium (I-Il) chloride, carbonyl-bis-triphenylphosphine-ro.ch di (1 bromide or dimesium-carbonyl-pentochloropropod (. Especially preferred are soda Rhodium and magnesium, such as Mgj EhCIfJg, which is produced by converting magnesium chloride with rhodium chloride in acetic acid with, or Mg |; Rh {CO) 2 Cipg, forming 11 | Ice from magnesium chloride and CBhCco) CI2J2 mixture methanol, chloroform and hydrogen chloride under nitrogen atmosphere. Also considered are rhodium compounds in which it is ionically or complexed with a carrier. For example, such are zeolite and ion exchangers with rhodium halides, as well as rhodium, complexed with magnesium silicate. In addition to magnesium, other metals, such as lithium, beryllium, calcium, manganese, iron, cobalt or nickel, may also be present in these compounds. The catalyst can be obtained by deposition on a carrier of catalytically active salts or complex compounds of monovalent or divalent rhodium, on which they are post-impregnated with a magnesium salt already active without reduction. It is also possible to use rhodium salts or complex compounds in which it is trivalent, and after impregnation, due to appropriate reduction, to obtain catalytically active rhodium salts in which rhodium is present at a valence below three, but not as a metal. This directed reduction can also be carried out under the conditions of synthesis gas conversion, i.e. reduction with a mixture of hydrogen and carbon monoxide. As the magnesium salts, simple organic and inorganic magnesium salts are used, for example, such as chloride bromide, nitrate, formic, acetate. It is also possible to use magnesium oxide, hydroxide or carbonates, if they are converted by treatment with mineral salts or carboxylic acids to the named salts. As the complex compounds, for example, the aforementioned magnesium-hydrogen complexes are particularly suitable. Magnesium compounds can be applied to the carrier along with the compounds of the clans. However, you can also apply cocatalytic esky magnesium onto the carrier before this or embed it into a frame substance, such as silica or aluminum, with a carrier such as silicic acid alumina or aluminosilicate. Considerable possibilities are that magnesium can be added with using ion exchange to the cation exchanger, which is also suitable as a carrier for rhodium and stable under the conditions of experimentation, for example, synthetic or natural aluminosilicates, known as molecular sieves. However, the impregnation of the carrier can be carried out in a different sequence, i.e. prior to the impregnation of the rhodium compound, and then with magnesium compounds on suitable catalysts. The halide is used in the form of the corresponding rhodium or magnesium compounds, as well as halogen-free role-playing or magnesium compounds, for example acetates or nitrates, and due to the subsequent treatment with hydrogen halide or impregnated with the metal halide, halogen ions are deposited on the carrier. It is also possible to use an organic compound containing halogen, such as, for example, 1,1-dichloroethane, from which halogen is released to regulate the halogen content on the catalyst, which is necessary for the selective conversion of synthesis gas after impregnation with a rhodium or magnesium compound. The method is carried out as follows. As catalyst supports, carriers with different specific surface areas are commonly used. Preferred are carriers with specific surfaces in the range of 50-1000. Suitable, for example, silicic acid, natural or synthetic silicates of elements of the I-VIII groups of the periodic system (as well as, for example, silicates of magnesium, calcium, aluminum, rare earth elements, titanium, zirconium, manganese ), then oxides of aluminum, titanium, zirconium, thorium zeolites and spinels. To prepare catalysts, the carriers simultaneously or successively one after another impregnate the asset. components. When using salts of trivalent rhodium, subsequent treatment with suitable reducing agents, such as hydrogen, carbon monoxide, methanol, is an essential step in the preparation of the catalyst. This reduction can be carried out in a separate apparatus or even in the reactor itself. While maintaining such conditions of recovery, in which rhodium acquires a lower valence (non-metal). For this, temperatures below 300 ° C are suitable, preferably in the range of lOO-ZTS C. It is advisable to repeatedly carry out the reduction not with dilute: gaseous reducing agents, but with gases containing additional amounts of inert gas, such as nitrogen carbon dioxide or noble gases. The concentration of rhodium, magnesium, or halides can be varied over a wide range in catalysts: values range from 0.1–20 wt.% For rhodium, 0.1–25 wt.% For magnesium and 0.01–20 wt.% For halide ions. Preferred are catalysts with a content of 1.0–10 wt.% Rhodium, 0.120 wt.% Magnesium and 0.05–15 wt.% G logides. For carrying out the process, a gas mixture consisting of all or substantially of carbon monoxide and hydrogen is used, which may also contain other cocktails such as nitrogen, argon, carbon dioxide or methane, and it is passed through a catalyst. The molar ratio of carbon monoxide to hydrogen can vary widely. Preferred are molar ratios in the ranges of 5: 1-1: 5, namely, in the ranges. Reaction temperature The wells lie in the range of 200-350 ° C, and reaction pressures are selected in the range of 1-300 atm, mainly in the range of 20-200 atm. It is advisable to coordinate the temperature and pressure with each other, which guarantees a high selectivity with respect to oxygen-containing compounds and, insignificantly, supports the exothermic formation of methane, which is favorable at higher temperatures. Therefore, high pressures and as low temperatures as possible are preferred. The degree of carbon monoxide conversion should not exceed 50%, since a higher degree of conversion can lead to an increased formation of by-products, and, along with methane, carbon dioxide and gaseous hydrocarbons, high molecular weight liquid hydrocarbons can also be formed. oxygen-containing products.
    A gas phase is preferred for carrying out the process. For this, conventional fixed bed reactors can be used / and for improved heat dissipation the thickness of the catalyst bed should be made negligible. Movable catalyst beds or fluidized bed reactors are also suitable.
    The synthesis gas conversion can be carried out in the presence of a solid and finely divided catalyst suspended in inert solvents and / or reaction products.
    A particularly preferred method of implementation is that the conversion is carried out in the gas phase using gas-circulating apparatus: the gas phase, after separating the condensable reaction products, is returned to the reactor again. This method is particularly economical and allows for dilute fresh gas with residual gas depleted in relation to hydrogen and returning to the circulation cycle, to maintain higher reaction temperatures and, thus, higher specific yields at constant selectivity:;. Apparatus with a gas circulation can be considered apparatus with an external and internal circulating gas.
    When carrying out the process, it was found that the catalysts exhibit a high initial activity and an excellent selectivity of the conversion of carbon monoxide to oxygen-containing C2 compounds, however, with long-term use of the catalyst. Those. with an operating time of approximately more than 500 hours, the activity and selectivity of the catalysts can gradually decrease. Therefore, catalysts have a limited service life.
    It has been found that this period can be significantly lengthened if in the process of converting the synthesis gas to the reaction zone, together with the gaseous components of the reaction, we continuously or permanently introduce magnesium salts or magnesium compounds evaporating under the reaction conditions. This preferred form of performance gives the advantages that the catalysts used for the conversion remain almost unchanged in terms of their selectivity and activity for more than 1000 hours.
    Salts or compounds of magnesium, ispa. : P1C1Ciez under reaction conditions, it is possible to introduce this into the regional zone together with one or more of the .Mtt reaction components in gaseous form: such compounds, for example, can be magnesium chloride, magnesium bromide, magnesium iodide, magnesium acetylacetonate, magnesium ethoxide, magnesium isopropyl, magnesium aluminomethylate and magnesium isopropylate, as well as magnesium salts of aliphatic monocarboxylic acids containing 1-4 carbon atoms in the molecule. Chloride or magnesium acetate is preferably used. However, it is also possible to use such salts or magnesium compounds which, due to the conversion with hydrogen halide, are converted into a halide or due to the conversion with aliphatic monocarboxylic acids, are converted into the corresponding carboxylates, for example, such as oxide, hydroxide or magnesium carbonates.
    Volatile salts and magnesium compounds are fed into the reaction zone along with the gaseous reaction components, and various methods can be used for this. Magnesium compounds can be injected over the catalyst bed in dissolved form, for example, as a solution in water, ethanol or acetic acid, into the hot gas stream. It is also possible to completely or partially, at an elevated temperature, bring the reaction gas into contact with the solution or melt of the magnesium compound before passing it into the reaction zone or pass this gas through the solution or melt. It is particularly preferable to pass all or part of the reaction components through the volatile magnesium compound, which is in a solid state, at elevated temperature. And, thus, evaporate the magnesium compound without using an additional solvent. For this purpose, also be applied on an inert carrier, for example, silicic acid, alumina or coal. The magnesium compound to be evaporated may be located inside or outside the reactor. Oba heated reaction components in the early pass zone containing a magnesium compound, and then the reactor zone containing the catalyst. In principle, these zones may P1vrehodit one another or depending on the circumstances be interleaved with each other.
    Magnesium volatile compounds can be fed to the reaction zone periodically or continuously. With a preferred continuous feed, the amount of magnesium compound is 0.01200 ppm, preferably 0.150 h, ppm, or the weight of the gas stream passing through the catalyst. When periodically introducing the compound magnesium-c, depending on the duration of the injection, it is possible to mix more gas to the C1-mixture. The amount supplied must be adjusted by the temperature and the volume of gas passed through the magnesium compound. The main stream containing volatile magnesium compound carbon monoxide hydrogenpur is then converted on a catalyst containing rhodium, magnesium, and a halide. With a particularly preferred method of execution in apparatus with compasses. After the separation of the condensable reaction products, the unconverted gas mixture after the addition of fresh synthesis gas is returned to the reactor, the magnet compound can be introduced either into the circulating gas, or into the fresh synthesis gas, or into a mixture of both of them. The service life of the catalyst can be extended not only by introducing magnesium compounds, but also by another method, namely, non-pertly or periodically introducing into the process of converting synthetic gas to the reaction zone, together with the gaseous reaction components, hydrogen halide or volatile organic halogen compounds. in the molecule and which, under reaction conditions, split the hydrogen halide. This preferred form of implementation of the method has the same advantage as the supply of magnesium compounds, i.e. the activity and selectivity of the catalyst used for the conversion remain approximately unchanged even after more than 1000 hours of operation. Hydrogen chloride, hydrogen bromide or hydrogen hydrogen or their mixture can be used as halogen hydrogen, or to receive, thanks to, the transformation of halogens with hydrogen or synthesis gas in the reaction space. Hydrogen chloride is a preferred hydrogen halide. Volatile organic halogen compounds not containing sulfur or nitrogen in the molecule and cleaving halogen-hydrogen under the reaction conditions are alkyl- and aralkyl halides with one or more halogen atoms in the molecule, such as, for example, dichloromethane, carbon tetrachloride, ethyl iodide 1.1 lichloroethane, allyl chloride, tert-butyl chloride or benzyl chloride, as well as saturated or unsaturated halogenocarboxylic acids, aldehyde alcohols or aliphatic, cycloaliphatic or aromatic esters, for example, mono-, and / or trichporoacetic acid, iodoacetic acid, bromoacetone, o (rj9-dichloro.ethyl ester, 3-chloro-crotonic acid (cis-or trans-1 and G7-chlorobenzoic acid. Also suitable are halides of carboxylic acids, for example, as acetyl chloride, bromide and iodide, or mono-di- or trichloro-acetyl chloride, which, under the action of water produced in the synthesis of synthesis gas, can easily be split off with hydrogen halide. The preferred organic halo compound is acetyl chloride. In order to significantly increase the service life of catalysts, it is not necessary that the removal of hydrogen halides from volatile organic compounds ga.pogenov occurred quantitatively, it is sufficient to already remove small quantities of hydrogen halogen a. Organic compounds that split one or more hydrogen halides together with the gaseous reaction components are introduced into the reaction zone, and various methods are used for this. Thus, it is possible to introduce hydrogen halides or organic halogen compounds in dissolved form, for example, as a solution in water, ethanol or acetic acid, into a hot gas stream. It is also possible to pass all of the reaction gas (or in a stream, only a part of this gas stream) through a solid or liquid organic halogen compound before introducing it into the reaction zone. Thanks to the choice of the amount of gas,. the temperature and pressure can accordingly bring the partial pressure of the supply connection to the desired level. It is also possible to apply an organic halogen compound in an impregnated form onto an inert carrier, such as silicic acid, alumina or coal, through which the reaction components are then passed, i.e. CO and Hj. Hydrogen halides or volatile organic halogen compounds can be introduced into the reaction zone continuously or intermittently. With preferred continuous feed in, their concentration is generally 0.01 to 500 ppm, preferably 0.1100 ppm, based on the weight of the gas stream passing through the catalyst. With peri-flow, depending on the length of the inlet, you can also add more gas mixture. At the same time, the added quantities are inversely proportional to the duration of the input. Then a gaseous stream containing halohydrocarbons or volatile organic halogen compounds, carbon monoxide and hydrogen, is circulated with Kt on a catalyst containing rhodium magnesium and a halide. In a particularly preferred embodiment of carrying out the process in a gas circulating apparatus, in which, after separating the condensable reaction products, the unreacted gas mixture after adding fresh synthesis gas is returned to the reactor, the hydrogen halide or organic halogen compound is added to either the circulating gas or fresh synthesis gas, or a mixture of both. Both described measures to extend the service life of catalysts, i.e. supplying compounds of magnesium or hydrogen halide, respectively, of an organic halogen compound, can be carried out simultaneously. Thus, the proposed method produces oxygen-containing carbon compounds, in particular, acetic acid, and / or acetaldehyde, as well as products that can be formed in successive reactions, for example, during esterification of OR concentration, from these products under reaction conditions with high selectivity. These include, among others, ethyl acetate and acetyldehyde diethyl acetal. The proportion of other oxygen-containing compounds with three or more carbon atoms in the molecule is very unstable and on average is less than 5 mol.% In terms of the reacted carbon monoxide. The overall selectivity with respect to the oxygen content of the AEPM Q-compounds, including the products grown in ethyl acetate and acetaldehyde diethyl acetal, is up to 90 in terms of the reacted carbon monoxide. The rest of carbon monoxide is transformed, except for the products with three or more carbon atoms, mainly in methane and other gaseous hydrocarbons, and also to a slight degree in carbon dioxide. General provisions of the experiment. The apparatus consists of a heated reaction tube with an internal diameter of 16 mm and a length of 1 m, made of corrosion-resistant steel / with a coaxially mounted thermometer sleeve with an outer diameter of 6 mm, a sequentially connected condenser, a condensate receiver and a Koneipeccopa for returning a part of the unconcentrated gaiter into the reactor (circulating gas). 100 ml of the catalysts described below are loaded into the tube. After flushing the equipment with nitrogen, the pressure of the synthesis gas is first set at 49 vol.% Co, 49 vol.% And 1. o6.% COji and 1% Njf and minor, quantities of other components), at 100 atm and the reactor is heated to. During the heating and during the course of the experiment, the circulating gas is supplied through the suction inlet of the compressor and, together with 450 nl / h of synthesis gas of the above composition, is passed through the catalyst. The gas mixture leaving the reactor is cooled approximately to a condenser which operates on a cooled brine approximately and the condensing part is collected in the receiver. The gassed off unconcentrated gas, after being mixed with fresh synthesis gas, is fed back through the compressor to the reactor. To maintain pressure and exclude any by-products, a portion of the residual gas is vented through the shut-off valve as exhaust gas. By this method, the catalysts described in the follow up are checked. 1 shows the time of the experiment, the specific yields of oxygen-containing C-products per liter of catalyst per hour at the beginning and at the end of the experiment, the percentage ratio of acetic acid, acetal, dehydrate and ethanol in terms of part of the condensate containing compounds with two carbon atoms in the molecule, and selectivity with respect to these compounds (in mol.% per converted c.; minor amounts of ethyl acetate or cetaldehyde diethyl acetaldehyde are converted into acetic acid, ethanol or acetaldehyde. According to catalyst emission Example: 40 g of silicic acid with a specific surface of 270 MVr, a pore volume of 1.22 ml / g, a bulk weight of 0.4 kg / l, pH 7.4 (measured on granules with a diameter of 23 mm), and content of 99.35 weight.V SiO and 0.2 weight,% Na is mixed with a solution of 7.5 g of magnesium sulfate (56%) in 45 ml of water, dried for 2 hours at and 2 hours at. Then it is sintered at during 30 minutes After cooling, mix with a solution of 5.7 g of Rhcljx H2.0 (37.8 wt.% Rh) in 45 ml of water and dry in the manner described above. The catalyst is reduced in a flow-through glass; a 1-tube at normal pressure, a temperature of 225-275 s and lowered over 3 hours 30 nl / h of hydrogen. After reduction, the catalyst contains 4.6 wt.% Rh, 2.3 wt.% Kg and, 4.9 wt.% CI. At the beginning of the experiment, the specific yield is 470 g of oxygen-containing Cj products per liter of catalyst per hour. The percentage distribution of products, wt.%: Acetic acid 60, acetaldehyde 32.8, and ethanol 7.2. After 620 hours of testing, the content of C is still 3.8% by weight. a) The catalyst does not contain magnesium and halogen. 6.1 g of Rh (N03) 2 "2H20 (31.8 wt.% Rh) are dissolved in 45 ml of water and n & n 40 g of the silicic acid carrier described in the example. The catalyst is kept for 2 hours and then dried at and 260 mA while passing 1 nl / h of nitrogen. The catalyst is reduced according to the method described in Example 1, after which it contains 4.6% by weight. Bh. , b) The catalyst is free of gal .ogen. 10.6 g of Mg (N02. La bN2 O are dissolved in 43 MP of water, applied onto 40 g of silica carrier shown in Example 1, csouaT is heated at and then for 30 minutes at. After, cooling is impregnated with solution 6 , 3 g of Rh (K03) 2) (31.8 wt.% Eh il in 45 ml of water, dried under vacuum (260 mAm and allowed to pass 1 nml / h of nitrogen and boiled as described in Example 1. After reduction the catalyst contains 4.6% by weight of Rh and 2.3% by weight of Mg. Example 2. A natural, commercially available magnesium silicate with a barely blowing composition,% by weight: SiO 56-60, ATgO3 1, is used as a carrier. 2-3,5, FejOj 0.5-1.3, MgO 22.0-26.3, total SC, 5.5-8.0, oxides of alkali metals, CaO and TiO2. The loss on ignition is 10 wt.%, The specific gravity is 2, 45-2.6 g / ml and grain size 23 mm 54 g (approximately 0.1 l) above the described carrier mix up with a solution of 7.0 g EhCl3 Hj.O (37.9 wt.% Rh) in 45 ml water and dried at 150 ° C. The catalyst is reduced as described in example 1, method. However, instead of 30 nl / h of hydrogen, 60 nl / h of a mixture of nitrogen and hydrogen are passed in a volume ratio of 1: 1. The reduced catalyst contains 4.6 wt. Rh, 13.5 wt.% Mg and 2.3 wt.% CI. After 450 hours of operation, the chlorine content in the catalyst is still 2.1 wt.%. Example 3. (recovery in the reactor). 54 g of approximately 0.1 l of cited in example 2 were mixed with a solution of 7.0 g of EhCl3 «H20 (37.8 wt.% Rh) in 45 ml of water and dried at l50c. 100 ml of this catalyst, without restoring, are introduced into the reactor and heated to 225 at atmospheric pressure and passing 30 nl / h of nitrogen and reduced at this temperature by passing 60 nl / h of a mixture of carbon monoxide and hydrogen through it in a volume ratio of 1: one. In contrast to the general description of the experiment, set at. the synthesis gas temperature is a pressure of 10 atm and then the catalyst is heated to a reak.ik temperature (215 ° C). After reduction, the catalyst. contains 4.6% by weight of Rh, 13.5% by weight of Mg and 2.25% by weight of C1. After 240 hours of operation, the chlorine content in the catalyst is still 2.0% by weight. Example 4. Natural carrier (described in Example 2) or magnesium silicate is punched and dried. After that, it has the following composition, wt.%: SiO 65,5; AI Oj 3.6, Fe Oj 0.5, and MgO 14.0. The bulk density is 537 g / l, the pore volume is 0.99 ml / n. 54 g of this carrier are squeezed with a solution of RhCIjX HjO (37.8 wt.% Rh) in 49 ml of water and suiat at. The catalyst is restored as described in example 1 method. Example 5. 54 g of the carrier prepared from example 4) from magnesium silicate is mixed with a solution of 14, 4 g of RhBr.ji2H20 (27.2 wt.% Rh) in 49 ml of water and dried. The reduction procedure is analogous to Example 1. Reduced catalysis contains, in wt.%, Rh 6.0, Mg 7.3, and Br 7.3. After 31 bch operation, the bromine content in the catalyst is reduced only to 6.6 wt.%. Example 6. 10 g of RhCIjXHjO (37.8% by weight of Rh) were dissolved in 20 ml of water, mixed with a solution of 18.2 g of potassium iodide in 20 ml of water upon cooling and immediately after mixing they were applied to 54 g of a carrier of silicate magnesium with a composition similar to that of example 4. The impregnated catalyst is kept for 48 hours at room temperature and then dried under vacuum in a nitrogen atmosphere at 80 ° C. After drying, it contains, wt%: Rh 4.6, Mg 5.5, K 5.2, I 16.9 and CI 4.7. The reduction is carried out according to the method described in example 1, passing at atmospheric pressure for 3 hours and temperature 225-275 ° C 30 nl / h of hydrogen. After reduction, the catalyst contains 4.7 wt.% CI and 5.6 wt.% J. Example 7. 40 g of the carrier described in example 1 is mixed with a solution of 4.4 g f; Rh (CO) 2 CIJz 52.94 weight Rh, Q g anhydrous magnesium acetate in 43 ml of methanol and dried at 80c. A catalyst containing 4.6% by weight of Rh, 2.3% by weight of Mg, and 1.9% by weight of Ci is placed in a reactor without pre-reduction treatment. Example 8. 40 g of the carrier described in example 1 is mixed with a solution of 9.1 g of MgjtRhCI JjJfTHjO (24.8 wt.% Rh, 8.8 wt.% Mp) in 45 ml of methanol, dried at 80 ° C and reduced as shown in example 1 method. After reduction, the catalyst contains, in wt.%: Rh 4.6, Mg 1.6. And CI 4.0.
    An example (method for preparing a catalyst using a freeze-drying method). 4.9 g of (CO) 2 CIJ2 (42.5 wt.% Bh) is dissolved in methanol under an aeote atmosphere and applied to 40 g of a cooled carrier made of acid; the composition is as in Example 1), cooled to and dried at a pressure of 13 atm to achieve a constant weight. Ready catalyst contains, wt%: Bh 4,6; Mg 0.55, CI 3.2. 100 ml of catalyst are introduced into the reactor without further reduction.
    Example 10. A calcined catalyst containing magnesium dichloride, prepared in accordance with Example 1, was impregnated with 2.4 g of RhCIjXHj, 0 (37.8% by weight of Pb) in 45 ml of water after cooling with a solution. After drying, the catalyst is reduced in the same manner as in Example 1. After reduction, the catalyst contains 2.0 wt.% Rh, 2.3 wt.% Mg and 3.8 wt.% C1.
    Example. The method described in Example 1 is used, however, a solution of 10.2 g of BhCIji H j is used for impregnation with RhCIj. About f37.8 wt.% Rh) and 45 ml of water. Further processing is carried out as in Example 1. The reduced catalyst contains 9.0 wt.% Rh, 2.5 wt.% Mg and 5.4 wt.% C1.
    Example 12. 40g of the carrier described in example 1 are impregnated from silicic acid with a solution of 7.5 g of magnesium dichloride (56% -NB1y) and 5.0 g of RhCl3xHj.O (37; 8 wt.% Rh) in 45 ml of water and dried for 2 hours at and 2 at. The catalyst is reduced as in example 1. The catalyst contains, after reduction, 4.0 wt.% Rh, 2.3 wt. % Mg and 4.3 wt.% CI.
    Make-up artist 13. 100 g of silicic acid with a specific surface of 270, a pore volume of 1/27 ml / g, a bulk weight of 0.4 kg / l, pH 7.4 | (in the form of granules with a diameter of 2-3 mm), as well as content of 99.35 wt.% SiOg and 0.2 wt.% Na is impregnated with a solution of 18.75 g of magnesium chloride (56%) in 112 ml of water and then dried for 2 hours at 70 ° C and 2 hours at. Then for 30 minutes, calcined at. After cooling, the silicic acid is impregnated with a solution of 14.25 g of RhCIji " HjO (37.8 wt.% Rh) in 112 ml of water and dried as described above. The catalyst is reduced in a glass flow tube at atmospheric pressure, 225-275 C, and passing a stream of hydrogen for 3 hours at a rate of 75, nl / h. The catalyst contained, after reduction, 4.6% by weight of Bb, 2.3% by weight of Mg, and 4.9% by weight of C1.
    100 ml of catalyst are placed in a vertical flow tube made of corrosion-resistant steel with an internal diameter of 16 mm and a length of 1 m serving as a reactor;
    0 which is provided with a salt bath for heating, a temperature measuring device connected in series by a cooler, a condensate receiver and a device
    c to reduce the pressure. After flushing, at 120 atm, the hourly flow rate of the gas mixture containing 49% by volume of carbon monoxide, 49% by volume of hydrogen, and 1% by volume of carbon dioxide and a small amount of nitrogen is passed through the catalyst. An aqueous stream of hot water is also introduced into the hot gas mixture in front of the reactor.
    5 0.07 wt.% Solution of magnesium acetate (10 ml / h). After exiting the reactor, the reaction gas is cooled to approximately + 5 ° C and the uncondensed portion is separated. As
    0 condensate forms approximately 27 g / h of acetic acid, 13 g / h of acetaldehyde and 4 g / h of ethanol in the form of an aqueous solution, which corresponds to the specific yield with respect to
    5 to these oxygen-containing Cr-products 440 g per liter of catalyst per hour. Insignificant amounts of about 2 wt.% In terms of the above C-products) formed in ethyl acetate or diethadedetal acetaldehyde are converted to acetic acid, ethanol or acetaldehyde and take into account in these values the same for subsequent examples,
    5 P °) The CO conversion is 39.5 vol.
    the selectivity with respect to oxygen-containing C-products is 82% in terms of converted carbon monoxide. After 1400 hours of work, the specific
    0 yields, CO conversion rate and selectivity are still unchanged. . .
    at). Work the same as in example 13, but instead of an aqueous solution
    5 mg acetate per pre
    the heater supplies 10 ml / h of distilled water, after 200 hours of operation, 440 g of oxygen-containing C2 products are also given, after about 550 hours of operation - 425 g, after 1000 hours of operation - 320 g per liter of catalyst per hour. The composition of Cz Products is the same as in Example 13. During this time, the conversion of CO decreases from 39.5 to 34.6% and the selectivity with respect to oxygen-containing Cj products from 82 to 68%. Example 14. The reactor described in example 13 was filled with 100 ml of the catalyst mentioned therein. The test procedure is the same as in Example 13, however, it is different in that a solution of magnesium acetate is not injected into the preheater. Instead, 100 ml of silicic acid is injected into the pre-heater, which is soaked in a solution of 20 g of magnesium chloride (56% in 35 g of water and then dried. The reaction components are carbon monoxide and hydrogen, having the same composition as in Example 13, with the reaction conditions described in example 13, 30.5 g / h of acetic acid, 10.5 g / h of acetaldehyde and 3.8 g / h of ethanol in the form of aqueous condensate are obtained. em 38.7%, the selectivity with respect to oxygen-containing. 2-products, 33.4% in terms of converted carbon monoxide. The specific yield, degree of CO conversion and selectivity still remain unchanged after more than 1200 hours of operation. Example 15. Natural, commercially available magnesium silicate is used as a carrier, which after washing and drying it has the following composition, wt%: SiOy 65.5, AlgOj 3.6, 0.5 and MgO 14.0. The bulk density is 537 g / l, the pore volume is 0.99 mg / l. 108 g of this carrier (200 ml) is impregnated with a solution of 12.6 BbCl1 H2.0 (37.8 wt.% Rh in 98 ml of water and dried at 150 s. The catalyst is reduced in a glass flow tube due to a 3-hour pass of 75 nl / h of nitrogen at 225-275 ° C and normal pressure. The catalyst contains, after reduction, 4.2% by weight of Rlx, 7.9% by weight of Mg, and 3.8% by weight of C1. 100 ml of reduced catalyst are introduced into the reactor described in Example 14 /, which is additionally provided with a compressor for circulating a portion of the residual gas mixture. The preheater is filled with 100 ml of silicic acid carrier, which has been soaked with a solution of 15 g of magnesium acetate in 400 ml of water and then dried. After flushing with nitrogen, first of all, the pressure of synthesis gas is set (49% by volume of CO, 49% by volume of H2, 1% by volume of COg and traces of KgjTpaBHoe 120 atm and the catalyst is heated to 280 ° C. During heating and with the further flow of experience by The circulating compressor is supplied with 300., NL / h syngas, and together with the circulating gas heated with a preheater to 280 ° C, is passed through the reactor. The gas mixture leaving the reactor is cooled to + 5 ° C with the brine-operated condenser and the condensing part collected in the receiver. The residual gas, after being mixed with fresh gas, is supplied by means of a compressor again to the preheater and the reactor. To maintain the pressure at a constant level and to prevent the formation of by-products, some of the residual gas is removed by means of a stop valve in the form of exhaust gases. 49 g / h of oxygen-containing Cj.-products (15 g of acetic acid, 6 g of acetaldehyde and 28 g of ethanol as an aqueous solution, respectively, the specific yield is 490 g / l per hour. The degree of CO conversion averages 35% of the starting product and selectivity for oxygen-containing C2 products of 86.6% based on converted carbon monoxide. The specific yield, CO conversion rate and selectivity remain unchanged after 1200 hours of operation. d) Operate as in Example 15, however, the preheater is filled with pure, non-impregnated silicic acid. Under the same experimental conditions as in example 15, when using 100 ml of catalyst, the specific yield is equal in the first 380 hours of work 475 g of oxygen-containing Cj products per liter of catalyst per hour, after 720 hours of work 435 g / l per hour after 1200 hours 360 g / l per hour with an equal percentage of the mixture of products specified in Example 15. The degree of CO conversion decreases at a named time from 35 to 28.6% and the selectivity decreases with respect to oxygen-containing Cj products from 86 to 77.9% in terms of converted carbon monoxide. Example 16. 100 g of silicic acid with a specific surface of 270, a pore volume of 1.27 ml / g, a bulk weight of 0.4 kg / l, pH 7.4 (in the form of granules with a diameter of 2-3 mm), as well as a content 99.35% by weight of Sio and 0.2% by weight of Na are impregnated with a solution of 14.7% magnesium chloride in. 112 ml of water and then dried for 2 hours at 70 ° C and 2 hours at 150 seconds. Then for 30 minutes, calcined at. After cooling, silicic acid is impregnated with a solution of 14.0 g of Ehcl x X (38.0 wt.% Rh) in 112 ml of water
    and dried as described above. The catalyst is reduced in a glass flow tube due to the 3-hour transmission of 75 nl / h of hydrogen at 225-275 s at atmospheric pressure. After reduction, it contains 4.5% by weight of Rh, 1.8% by weight of Mg and 4.7% by weight of C1.
    100 ml of catalyst are placed in a vertical flow tube made of stainless steel with an inner diameter of 16 mm and a length of 1 m, serving as a reactor, which has external heating with a salt bath, a temperature measuring device, a connected refrigerator, a condensate receiver and a device for reducing pressure.
    After washing, the catalyst is passed at 100 atm and 320 nl / h of a gas mixture consisting of 49% by volume of carbon monoxide, 49% by volume of hydrogen, 1% by volume of carbon dioxide and an insignificant amount of nitrogen. An aqueous 0.1 wt.% Hydrochloric acid (10 ml / h), also heated to 290 ° C, is introduced into the hot gas mixture before the reactor using a pre-heater.
    After exiting the reactor, the reaction gas is cooled to approximately and the non-condensed part is separated. Approximately 34 g / h of acetic acid, 8 g / h of acetaldehyde and 4.5 g / h of ethanol in the form of an aqueous solution are collected in the form of condensate, cc5, respectively, the specific yield of these oxygen-containing Ct-products is 465 g per liter of catalyst per hour. Minor amounts (approximately 2 wt.% In terms of the above Cjp products) of ethyl acetate or acetaldehyde diethyl acetal are converted into acetic acid, ethanol or acetaldehyde and taken into account in these values. C This also applies to the following examples).
    The conversion of CO is 30 mol.%, The selectivity for oxygen-containing C-products is 80.6% based on converted carbon monoxide. After 1450 hours of operation, the specific yield is still 450 grams per liter of catalyst per hour. Selectivity remains unchanged.
    e) They work in the same way as in Example 16; however, instead of dilute hydrochloric acid, 10 ml / h of distilled water is fed into the pre-heater. After 200 hours of operation, the specific yield is also 465 g of oxygen-containing Cj products, after 750 hours of operation 410 g, and after 1200 hours only 370 g per liter of catalyst per hour. The percentage composition of C | -products is the same as in 16. The degree of conversion of CO decreases during this time from 30 to 27.5% and the selectivity for oxygen-containing products is 80.6 69.6%.
    Example 17. Natural, commercially available magnesium silicate was used as a carrier.
    . which after washing and drying has the following composition, wt.%: SiOj. 65.5, AlgO 3.6, FejiOj-0., 5 and MgO 14.0. The bulk density is 538 g / l, the pore volume is 0.99 ml / g. 108 g of this carrier (200 ml) are impregnated with 15 solution
    5 12.6 g of RhCIj X HgO (37.8 wt.% Rh) in 98 ml of water and dried at 150 s. The catalyst is reduced in a glass flow tube due to a 3-hour transmission of 75 nl / h of nitrogen at
    0 225-275 ° C and atmospheric pressure. After reduction, it contains 4.1 wt.% Rh, 7.5 wt.% Mg and 3.6 wt.
    C1. .
    100 ml of reduced catalysts are placed in the reactor described in Example 16, which is additionally provided with a compressor for circulating a portion of the residual gas mixture. After baking the bunker, first
    0, the pressure of synthesis gas (49 vol.% CO, 49 vol.% H, 1 vol.% CO2, traces of nitrogen) equal to 100 atm h is heated. The catalyst is up to. In the process of warming up and with further
    5 during the experience with the compressor
    350 nl / h of synthesis gas is supplied for circulation and, together with the circulating gas, is initially passed through the reactor. To preheater
    0 serves 18 ml / h of a 0.3% solution of methylene chloride in methanol. The gas mixture leaving the reactor is cooled to approximately + 5 ° C and the condensed portion is collected in the receiver. The uncondensed residual gas, after being mixed with fresh gas by means of a compressor, is again passed through a pre-heater and reactor. To maintain pressure at a constant level
    0 and avoid the formation of side
    products, part of the residual gas is emitted into the atmosphere through a stop valve. 48 g / h of oxygen-containing Cj-products (14 g of acetic acid, 5 g of acetaldehyde and 29 g of ethanol) are collected in the form of an aqueous solution, which corresponds to a specific yield of 480 l / l h.
    0 averages 32% of the starting product, selectivity for oxygen-containing C2 products is 79.6% based on converted carbon monoxide. The specific output, CO conversion rate and selectivity remain unchanged after 1750 hours of operation. e) They work according to the method described in example 17, but 18 ml / h of methanol is metered in to the preliminary heater. Under the same experimental conditions and using 100 ml of the catalyst of the composition mentioned in Example 1, the specific yield in the first 400 hours of operation is. 470 g of oxygen-containing C2-products per liter of catalyst per hour, 800 hours of operation, this value gives up to 460 g / l h and after 1250 hours of operation it is 425 g / l h at the same; The percentage composition of the products of the mixture, as in Example 17. The degree of CO conversion decreases in the indicated time from 31 to 39.5% and the selectivity to oxygen-containing products decreases from 80.5 to 76.5% in terms of converted carbon monoxide. Example 18. The method described in Example 17 is used, but 25 ml / h of diethyl ether are introduced into the preheater instead of the methanol solution of methylene chloride. The specific yield with respect to oxygen-containing C2-products is reduced under the same conditions from 490 g / l h for barely 100 hours of work up to 450 g / l h after 800 hours of work. With further pro- tection process, 25 ml of a 0.2 wt.% Solution of acetyl chloride in diethyl ether are fed to the pre-heater. At the same time, the specific yield remains almost constant and; after 1800 hours of operation, 440-445 g. per liter of catalyst per hour. Example 19. 40 g of silicic acid as described in example 1 is impregnated with a solution of 12.2 g of potassium hexahydrate chloride-magnesium in 45 ml of water, dried for 3 hours and then calcined for 30 minutes. After cooling, it is impregnated with a solution of 5.7 g of RhCIj X (37.9% by weight of Rh in 45 ml of water, dried at 70 ° C 2 .4 and another 2 hours at. The catalyst is reduced, as in Example 1, with a 3-hour treatment with hydrogen, skipping at a rate of 30 nl / h of 225-275 C at atmospheric pressure. The resulting catalyst contains, after reduction, 4.4 wt.% Rh, 2.2 wt.% Mg and 4.8 wt.% CI,. 20. Work similar to Example 19, however, instead of a solution of potassium chloride / magnesium in water, a solution of 1 g of acetylacetic magnesium in 45 ml of hot ethanol is used. After the reduction, the catalyst contains 4.9 wt.% Rb, 0.25 wt.% Mg and wt.% CI., Example 21. Analogously to Example 19 works, however, 4.4 g of dikshiy magnesium salt is used instead of chlorine potassium magnesium. ethylene diamite tetraacetic acid (X. The catalyst, reduced at 225-275 s, contains 4.8 wt.% Rh, 0.24 wt.% Mg and 2.8 wt.% CI. 100 ml portions of the catalysts described below (examples 22-33) are placed in a tubular reactor with an internal diameter: 16 mm and a length of 1 m, equipped with an external heating in the form of a salt bath, a device for measuring temperature, connected in series by a refrigerator, The Data for condensate and apparatus for bleed excess pressure. Nin After flushing with nitrogen, 170 nl of a gas mixture consisting of carbon monoxide and hydrogen in a 1: 1 volume ratio under hour is passed through the catalyst under the conditions indicated in Table 2. 2. Condensate and off-gas are analyzed by gas chromatography. In tab. Table 2 shows the data on the composition of the catalyst, the conditions of the reaction, the volume outputs obtained per experiment in the course of time, and the selective effect with respect to the reacted carbon monoxide. Example 22 (20 atm, 350 ° C, 1% yield). 100 g of silicic acid with a bulk weight of 0.42 kg / l and a surface according to UT 270 is impregnated with a solution of 2.2 g of MgCl x HjO in 110 ml of water, dried for 2 hours at 80 ° C and 2 hours U) and 15 ° C, then 30 are sintered min at 80 wasps. After cooling, the carrier is impregnated with a solution of 2.6 g. RhCIj X (37.8 wt.% Rhodi) in 110 ml of water and extract the powder exactly as described in wine. The catalyst is reduced by 3 hours nponygkaniem 50 nl / h of hydrogen at 250 ° C and atmospheric pressure. The catalyst contains 1 wt.% Rod. Of25% magnesium and 0.6% chlorine. PRI e R 23. (200 ATM, 9.5% of birth). The catalyst was prepared analogously to example 22, however, using a solution of 29 g of RhCIj x X (37.8 wt.% Rhodi) in 110 ml of water. The reduced catalyst contains 9.5% by weight of rhodium, 0.22% of magnesium, and 4.1% of chloride. Example 24 (Calcium chloride is added to a catalyst that does not contain halogen). 40 g of the halogen-free catalyst described in Example 1b are impregnated with a solution of 3.0 g of chloride after reduction. calcium in 45 ml of water and dried for 2 hours at and 2 hours at 120 ° C. The catalyst contains 4.2 wt.% Rhodi,., 2.0% magnesium and 4.0% chlorine. Example 25 (Supplement to. The catalyst that does not contain halogen
    40 g of the catalyst described in example 16, after reduction, is impregnated with a solution of 1 ml of hydrofluoric acid in 45 ml of water and dried for 2 hours at. The catalyst contains 4.5% by weight of rhodium, 2.2% magnesium and 1.5% fluorine.
    Example 26 (insignificant halogen concentration). Work similarly to example 24 and 25, however, the catalyst, which does not contain halogen, after reduction, is impregnated with a solution of 2.5 ml of 1% hydrochloric acid in 45 ml of water, then dried for 2 hours at and 2 hours at. The catalyst contains 4.5 wt.% Rhodium, 2.2% magnesium, and 0.05% chlorine.
    Example 27. (high halogen concentration). A solution of 24 g of MgCl c6HgO in 50 ml of 10% hydrochloric acid is applied to 50 g of silicic acid described in Example 22, then the carrier is dried for 2 hours at 2 ° C and 2 hours. After that, impregnated with a solution of 4.0 g of H, 0 C 37.8 wt.% Rhodium) in 55 ml of 10% hydrochloric; acid, dried as described above, and reduced by passing 3 hours 30 nl / h of hydrogen at atmospheric pressure. The catalyst contains 2.3 wt.% Rhodi, 3.4%; magnesium and 14.5% chlorine.
    Example 28: carrier variant) 100 g of aluminum makhany in the form of balls (2-4 mm in diameter) with a specific surface of 100 m / g and a bulk weight of 0.8 kg / l are impregnated with a solution of 8 g. EhCIj X HgO (37.8% by weight of rhodium in 45 ml of water and dried for 2 hours at 2 hours and at 150 ° C. Then the catalyst is reduced by passing 3 hours at 50 nl / h of hydrogen at 250 ° C. The catalyst contains 2.8 wt.% rhodium, 16.3 wt.% magnesium and 1.4% chlorine.
    Example 29 (option of carrier) 100 g of alumina in the form of balls with a meter of 2-5 mm with a specific surface of 350 MVr and a bulk weight of 0.77 kg / l are impregnated with a solution | 5 g of MgCIj, X 6HjiO in 45 ml of water, dried for 2 hours at 2 hours and then sintered for 800 minutes at 800 seconds. After cooling down, they are impregnated with a solution of 8 g of RhCIj X (37.8% by weight of rhodium) with 45 ml of water and dried as described above. In conclusion, the catalyst is reduced by a 3-hour pass, using 50 nL / h of hydrogen at 250 ° C. After reduction, the catalyst. holds 2.8 wt.% rhodium, 0.5% magnesium 5 and 1.4% chlorine.
    Example 30. (option carrier Catalyst prepared analogously to example 29, however, using 100 g of aluminum silicate containing.,
    0 13.0 wt.% AIjiOj and 86.5 wt.% SiO having a specific surface of 100 m UG, bulk density 0.75 kg / l. For the preparation of aqueous solutions of MgCIjr X or BhCl 3 use
    5 times 28 ml of water. The reduced catalyst contains 2.8% by weight of rhodium,: 0.5% magnesium and 1.7% chlorine.
    Example 31 (carrier variant) The catalyst is prepared analogously to example 29, however, using 100 g of zeolite in the form of sticks, containing pores with a diameter of 4-5; having a surface area of 420 and a bulk weight of 0.7 kg / l. Catalyst
    5 (in reduced form) contains 2.8 wt.% Rhodium, 0.5 mg and 1.5% chlorine.
    Example 32 (option media). As a carrier use
    Q 100 g of titanium dioxide in granular form with granules with a diameter of 1.23, 0 mm and a bulk weight of 0.7 kg / l. A catcher is prepared according to example 28, however, using 70 ml of water each time to prepare a solution of MgCl or x, rhodium trichloride. The reduced catalyst contains 2.75 wt.% Horn, di, 0.5% magnesium and 1.65% chlorine.
    Example 33 (carry version 0 l). As a carrier, 100 g of zirconium dioxide with a bulk weight of 1.86 kg / l and a surface area of 50 are used. The catalyst is prepared: 1 as described in example 28, however, "for the preparation of solutions of MgClg x NeO2 or rhodium trichloride, each time 20 ml of water is taken. The reduced catalyst contains 2.82% by weight of rhodium, 0.52% magnesium and 1.5% chlorine.
    0 The proposed method allows to reduce the selectivity of the process by others 6890% versus 60% in the known method, as well as to increase the productivity in individual cases (cases up to 450-532 g / LP
    5 vs 432 l / g-h in a known way.
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    权利要求:
    Claims (4)
    [1]
    1. METHOD FOR PRODUCING ACETIC ACID, ETHANOL, ACETALDEHYDE AND THEIR DERIVATIVES by reacting carbon monoxide with hydrogen in the presence of a rhodium-containing catalyst on a support at a temperature of 200350 ° C and a pressure of 20-200 atm, characterized in that, p. whole increases in the selectivity of the process, as the rhodium-containing catalyst, use the rhodium-magnesium-halogen complex compound, or rhodium and magnesium halides, or the rhodium halide and magnesium halide alkaline complex compound, or the rhodium halide and silicate, or acetyl acetate, or aluminate 'magnesium, or rhodium and magnesium nitrate and halogen hydrogen, or calcium or tin, or chromium chloride, or dimeric rhodium dicarbonyl chloride and magnesium acetate, with the rhodium valence in all compounds being 1 and / or 2.
    [2]
    2. The method according to π. 1, characterized in that in the process a catalyst is used, obtained by reduction of trivalent rhodium compounds at 225-275 ° C to rhodium compounds with valencies 1 and / or 2.,
    [3]
    3. The method according to π. 1, characterized in that a salt or magnesium compound is supplied continuously or periodically to the process together with the starting components in the process.
    [4]
    4. The method according to π. 1, with the fact that in the process, continuously or periodically, together with the starting components, hydrogen halide or an organic halide-containing compound is fed, which gives hydrogen halide in the process.
    Priority on points:
    04/04/78 by π. 1 10.06.78 p. 2 18.11.78 p. 3
    SU, .. 1064864
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    同族专利:
    公开号 | 公开日
    US4288558A|1981-09-08|
    AU522697B2|1982-06-24|
    DD142706A5|1980-07-09|
    EP0004653A1|1979-10-17|
    PL214644A1|1980-01-02|
    DE2960477D1|1981-10-22|
    CA1117140A|1982-01-26|
    PL120510B1|1982-03-31|
    JPS54141705A|1979-11-05|
    AU4574979A|1979-10-11|
    EP0004653B1|1981-07-15|
    引用文献:
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    US4482647A|1981-12-03|1984-11-13|National Distillers And Chemical Corporation|Manufacture of oxygenated compounds|
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    WO2014114822A1|2013-01-24|2014-07-31|Abengoa Bioenergía Nuevas Tecnologías, S.A|Promoted rhodium catalyst for the selective conversion of synthesis gas into ethanol|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19782814365|DE2814365A1|1978-04-04|1978-04-04|Catalyst for acetic acid, ethanol and acetaldehyde mfr. - from synthesis gas, consists of rhodium on support with co-catalyst of magnesium cpd. and halide ions|
    DE19782825495|DE2825495A1|1978-06-10|1978-06-10|Catalyst for acetic acid, ethanol and acetaldehyde mfr. - from synthesis gas, consists of rhodium on support with co-catalyst of magnesium cpd. and halide ions|
    DE19782850110|DE2850110A1|1978-11-18|1978-11-18|Catalyst for acetic acid, ethanol and acetaldehyde mfr. - from synthesis gas, consists of rhodium on support with co-catalyst of magnesium cpd. and halide ions|
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