Method of obtaining carbonyl compounds c2-c4

FIELD: chemistry.

SUBSTANCE: invention relates to method of obtaining carbonyl compounds, namely ketones and aldehydes C2-C4, which find different application as valuable semi-products of FINE and basic organic synthesis, as well as are widely applied as solvents. Method is carried out in gas phase by interaction of nitrous oxide with mixture of aliphatic C2-C4 olefins and alkanes at temperature 300-550°C and pressure 1-100 atm.

EFFECT: method makes it possible to obtain valuable target products with high productivity and high total selectivity with explosion safety of work.

12 cl, 4 tbl, 30 ex

 



 

Same patents:

FIELD: chemistry.

SUBSTANCE: one of method versions is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification and possibly partial recycling into reaction zone(s) of one or several components of reaction mixture. Decomposition is carried out in presence of inert easily-boiling solvent, which contains mainly hydrocarbons, whose boiling temperature is lower than 70°C, preferably lower than 40°C, but not lower than minus 1°C, which is partially evaporated directly from reaction zone(s) and partially distilled from obtained reaction mixture, is in liquid state returned to reaction zone(s) with supporting in it (them) temperature from 1 to 70°C, preferably from 10 to 45°C. Second method version is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification. Applied is easily-boiling solvent, which after separation from reaction mixture, possibly with part of ketone, is recycled into reaction zone(s), and sulfocationite catalyst in H+ form, resistant in liquid media, containing alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons in large amount, at temperatures up to 70°C, in fine-grain or coarse-grain form, possibly, in form of mass-exchange filling with size from 1.5 to 25 mm.

EFFECT: obtaining phenol and ketones without formation of large amount of by-products and resins and practically without equipment corrosion.

14 cl, 1 dwg, 6 ex

FIELD: industrial organic synthesis.

SUBSTANCE: in presence of a process for production of methyl ethyl ketone widely applicable in petroleum processing and petrochemical industries at oil dewaxing and paraffin deoiling plants, in varnish-and-paint industry to produce polyurethane coatings, in wood processing industry to produce a variety of glues, in industrial rubber article industry, in perfumery, and in other areas. Process comprises 2-butanol/hydrogen peroxide reaction conducted at 20-100°C and butanol/peroxide molar ratio (1.0-13.0):1 on titanium silicate catalyst having MFI, MEL, or beta zeolite topology and containing 0.1 to 9.5% titanium, content of catalyst ranging from 0.01 to 20% based on the total weight of reaction medium. Thus formed methyl ethyl ketone is isolated from reaction medium via rectification in the form of azeotrope with water while unreacted 2-butanol with admixture of water is recycled to synthesis stage. Methyl ethyl ketone/water azeotrope is separated via extraction with organic solvent as extractant at extractant-to-azeotrope ratio (0.5-10):1 and number of extraction steps from 1 to 10. Extract is separated via rectification or distillation processes to recover commercial methyl ethyl ketone while returning extractant to separation stage.

EFFECT: increased yield of methyl ethyl ketone and reduced power consumption.

2 cl, 1 tbl

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of 3-bromoadamantyl-1-alkyl(aryl)-ketones of the general formula: , wherein that can be used as intermediate substances for synthesis of some biologically active compounds. Method involves interaction of 1,3-dehydroadamantane with α-bromoketones of the following order: α-bromoacetone, α-bromoacetophenone, α-bromocyclohexanone in the mole ratio of reagents = 1:(2-3), respectively, in absolute diethyl ether medium, at temperature 34-40°C for 3-4 h. Method provides preparing the claimed compounds with high yield.

EFFECT: improved method of synthesis.

3 ex

FIELD: main organic synthesis.

SUBSTANCE: proposed method is used for production of ketones, for example dimethyl ketone (CH3COCH3), methyl ethyl ketone (CH3COC2H5) by direct catalytic oxidation of respective alkenes, for example propylene, n-butenes, as well as catalysts for realization of this method. Oxidation of alkenes is performed in the presence of metallocomplex catalysts containing organic component where nitrogen oxide (I) is used as oxidant. Used for process is catalyst on base of peroxopolyoxo metallate complexes of terakis (oxo diperoxo metallate)-phosphate (3-) together with quaternary ammonium cationes having formula Q3{PO4[MeO(O2)2]4}, where Me-Mo, W,V; Q3 is quaternary ammonium catione containing alkyl chains C4-C8 or N-hexadecyl pyridinium.

EFFECT: enhanced selectivity of process.

10 cl, 14 ex

FIELD: industrial organic synthesis and catalysts.

SUBSTANCE: invention relates to a methyl ethyl ketone production process via catalytic oxidation of n-butenes with oxygen and/or oxygen-containing gas. Catalyst is based on (i) palladium stabilized with complexing ligand and (ii) heteropolyacid and/or its acid salts, in particular molybdo-vanado-phosphoric heteropolyacid having following composition: H11P4Mo18V7O87 and/or acid salt Na1.2H9.3Mo18V7O87, said complexing ligand being notably phthalocyanine ligand. Catalyst is regenerated by making it interact with oxygen and/or oxygen-containing gas at 140-190°C and oxygen pressure 1 to 10 excessive atmospheres. Oxidation of n-butenes is conducted continuously in two-stage mode at 15 to 90°C in presence of above-defined catalyst.

EFFECT: enhanced process efficiency due to increased stability of catalyst resulting in considerably increased productivity and selectivity.

7 cl, 1 dwg, 3 tbl, 8 ex

The invention relates to the field of organic synthesis, namely the method of producing ethyl ketone by catalytic oxidation of n-butenes with oxygen, and the catalyst for its implementation

The invention relates to a method for producing methyl ethyl ketone, which is widely used as a solvent perchlorovinyl, nitrocellulose lacquers and adhesives

The invention relates to the production of lower ketones liquid-phase dehydrogenation of secondary alcohols in the presence of a fixed catalyst - Nickel metal or activated hydrogen Nickel metal or Nickel on the carrier in the environment paraffins C12-C20that process is used as solvent, the drying means, the environment for the activation of the catalyst and carrier

FIELD: chemistry.

SUBSTANCE: invention relates to a separation method intended for removing acetone from a mixture comprising acetone, methyl acetate and methyl iodide. The method includes the following steps: (a) feeding said stream comprising acetone, methyl acetate and methyl iodide into a first distillation zone; (b) feeding acetic acid into said first distillation zone, either by addition of acetic acid to said stream comprising acetone, methyl acetate and methyl iodide or by feeding acetic acid directly to the first distillation zone at one or more points at or above the point of feeding said stream comprising acetone, methyl acetate and methyl iodide into the first distillation zone at step (a), or a combination of both; (c) removing from the first distillation zone a light fraction stream comprising methyl iodide and a heavy fraction stream comprising acetone, methyl acetate, acetic acid, and a reduced amount of methyl iodide; (d) feeding into a second distillation zone the heavy fraction stream from step (c); (e) removing from the second distillation zone a light fraction stream comprising methyl acetate and methyl iodide and a heavy fraction stream comprising acetone, methyl acetate and acetic acid; (f) feeding the heavy fraction stream from step (e) into a third distillation zone; and (g) removing from the third distillation zone a light fraction stream comprising methyl acetate and acetone and a heavy fraction stream comprising methyl acetate and acetic acid.

EFFECT: invention relates to a method of producing acetic anhydride or combined production of acetic anhydride and acetic acid.

24 cl, 1 dwg, 1 ex, 1 tbl

FIELD: explosives.

SUBSTANCE: method to produce isopropanol is carried out in process of at least two reaction stages of hydrogenation, at the same time each reaction stage includes a reaction zone of hydrogenation, where the hydrogenation product released from the reaction zone of the first reaction stage contains a non-reacted acetone, and a flow of products containing acetone and isopropanol is supplied into the reaction zone of the next reaction stage, at the same time the specified flow of products at the inlet to the reaction zone of the specified next stage has temperature from 60 to 100°C. At the same time the temperature of the flow of products released from the reaction zone of the specified next reaction stage, at the outlet of the specified reaction zone is at least by 40°C higher than the temperature of the flow of products arriving into the specified reaction zone at the inlet to the specified reaction zone, and the temperature in the specified next reaction zone does not exceed 125°C.

EFFECT: method makes it possible to produce isopropanol of high degree of purity.

23 cl, 2 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention refers to the way of production of phenol, acetone and α-methylsterene, and to the installation for its implementation. The way consists in decompounding of cumene hydroperoxide and dimethylphenyl carbinol that are included into the technical cumene hydroperoxide, in the solvent with the presence of heterogeneous catalyst by means of catalytical distillation in the continuous isothermal mode at the boiling point of the solvent and with the latter's recirculation; as a solid heterogeneous catalyst, heteropoly acid H3PW12O40 or caesium-displaced salt of heteropoly acid Cs2.5H0.5PW12O40 is applied on the silicon dioxide, and as a solvent, acetone is employed. As a bearer, mesoporous silicon dioxide of MCM-41 grade is used, and decompounding of the cumene hydroperoxide and dimethylphenyl carbinol is carried out in two stages; the first stage stipulates decompounding of cumene hydroperoxide thus releasing phenol and acetone, and the second one - of dimethylphenyl carbinol thus releasing a-methylsterene; the mesoporous silicon dioxide and heteropoly acid or caesium-displaced salt of the heteropoly acid are used with the following component ratio, weight %: heteropoly acid - 10-50; silicon dioxide - the rest; or caesium-displaced salt of the heteropoly acid - 10-20; silicon dioxide - the rest.

EFFECT: decompounding of the cumene hydroperoxide and dimethylphenyl carbinol with 100 % conversion and 100 % selectance.

8 cl, 1 dwg, 8 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of decomposing cumene hydroperoxide with an acid catalyst to phenol and acetone in the system of a hollow reactor with back-mixing and swirling motion of reaction products, cooling the decomposition reaction mass in a cooling heat exchanger, using a catalyst system in form of 0.3-0.5 wt % solution of sulphuric acid in acetone, while feeding the catalyst into suction line of a circulating pump in the medium of the reaction mass, regulation of residual content of hydroperoxide at the end of the back-mixing cycle using a "control decomposition tube", in which a small portion of the reaction mass is mixed with the whole amount of the acid catalyst fed into the decomposition system, decomposition of the reaction products output from the back-mixing system by heating, holding in a structured flow apparatus and stepwise reduction of acidity in said apparatus by feeding water at the end of the first quarter of the length of the apparatus and fast cooling of the reaction mixture at the output of the structured flow apparatus. The volume of the hollow reactor in the back-mixing system is equal to or greater than the volume of the inter-tube space of the cooling heat exchanger of the reaction mass, wherein a constant amount of a portion of the acid catalyst per constant amount of the reaction mass is fed into the "control decomposition tube", the remaining portion of the catalyst through the flow regulator from the temperature difference at the ends of the "control decomposition tube" is directly fed into the suction line of the circulating pump, and mixing the decomposition reaction mass with the acid catalyst at the input of the tube with structural length in order to reduce the distance from the point of contact of the decomposition reaction mass with the catalyst to the first thermocouple of the "control decomposition tube".

EFFECT: invention enables to conduct a high-selectivity process for decomposition of cumene hydroproxide.

2 tbl, 2 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing phenol and acetone through acid-catalysed decomposition of cumene hydroperoxide in series-connected reactors in two steps at high temperature with simultaneous formation of dicumyl peroxide at the first step followed by its decomposition in a reaction medium at the second step. The process is carried out using a catalyst in form of 2-hydroxy- benzene sulphonic acid of general formula , where X and Y denote hydrogen, alkyl, arakyl, halogen, oxyalkyl, sulpho group, alkyl(2-hydroxy benzene sulphonic acid group) in amount of 0.1-1 mmol/l.

EFFECT: method enables to obtain desired products with high output while maintaining low content of hydroxy acetone in the reaction mass.

2 cl, 9 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of purifying acetone obtained together with phenol during decomposition of cumene hydroperoxide. The method involves distillation of crude acetone successively in three distillation columns. Low-boiling impurities are separated in the first distillation column with addition of an alkaline reagent into the column and then extracting the remaining mixture of components in form of a bottom product and feeding it into the second distillation column for separation of high-boiling impurities and extraction of the larger portion of acetone in form of commercial-grade acetone. Content of acetone in the still of the second distillation column is kept at a level not lower than 0.5 wt % of the supply by extracting the remaining components of the mixture in form of a bottom product of the second distillation column and then feeding into the third distillation column in order to separate the remaining acetone together with the remaining low-boiling impurities, including the remaining aldehydes and feeding this mixture into the first distillation column. An additional alkaline reagent is fed into the second distillation column which enables production of acetone having permanganate oxidation time of not less than nine hours. The alkaline reagent is fed into the first distillation column in form of a 0.1-30 % aqueous solution in amount of 0.05-0.8 wt % of the supply, and an oxidative reagent is also added in form of a 0.1-30% aqueous solution in amount of 0.02-0.5 wt % of the supply in weight ratio of the alkaline reagent to the oxidative reagent between 1:0.1 and 1:100, preferably between 1:0.5 and 1:10; the alkaline reagent is also fed into the second distillation column in amount of 0.03-0.5 wt % of the supply and the ratio of the alkaline reagent fed into the first column to the alkaline reagent fed into the second column is 1:0.2, wherein the second and third columns are used at atmospheric pressure.

EFFECT: disclosed method enables production of high-quality acetone with minimal operational costs and achieving maximum possible output.

9 cl, 2 tbl, 1 dwg, 13 ex

FIELD: chemistry.

SUBSTANCE: crude acetone is successively distilled in two distillation columns, whereby in the first distillation column low-molecular impurities are separated with addition of an alkaline reagent into the column and then extracting the remaining mixture of components in form of a bottom product and feeding it into the second distillation column for separation of high-molecular impurities and extraction of commercial-grade acetone. An alkaline reagent is fed into the second distillation column higher than the feeding point, which enables production of acetone with permanganate oxidation time of not less than 8 hours. The alkaline reagent is fed into the first distillation column in form of 0.1-30 wt % of an aqueous solution in amount of 0.05-0.8 wt % of the substance fed into the column. An oxidative reagent is also fed into the first distillation column in amount of 0.02-0.5 wt % of the substance fed into the column with weight ratio of the alkaline reagent fed into the first column to the oxidative reagent between 1:0.1 and 1:100, preferably between 1:0.5 and 1:10. An alkaline reagent is also fed into the second column higher than the feeding point in amount of 0.03-0.5 wt % of the substance fed. The weight ratio of the alkaline reagent fed into the second column to the alkaline reagent fed into the second column lies between 1:0.1 and 1:0.5. The second distillation column is used at atmospheric pressure.

EFFECT: method enables production high-quality acetone with maximum use of existing equipment and reagents, with minimum capital expenses on modernisation.

7 cl, 2 tbl, 1 dwg, 13 ex

FIELD: chemistry.

SUBSTANCE: method of processing carbon-carbonate mineral involves burning limestone in a reactor, obtaining calcium oxide, production of calcium carbide by reacting part of calcium oxide obtained from burning limestone with carbon, bringing part of the obtained calcium carbide into contact with water, obtaining acetylene and caustic lime, bringing gaseous wastes from burning limestone into contact with water to obtain carbonic acid. Limestone is burnt using heat obtained from burning part of the volume of acetylene, obtained from part of the volume of calcium carbide. At least part of the obtained acetylene is used in synthesis of ethanol and/or dichloroethane and/or ethyleneglycol and/or acetone. During synthesis of ethanol and/or dichloroethane, acetylene is reacted with hydrogen in the presence of palladium as catalyst, after which at least part of synthesised C2H4 material is reacted with water vapour, obtaining ethanol, and/or reacted with chlorine, obtaining dichloroethane. Also at least part of the obtained acetylene is subjected to hydrolysis, obtaining ethyleneglycol. Also during synthesis of acetone, part of the obtained acetylene is reacted with water vapour, where the hydrogen obtained is used in said synthesis of ethanol and/or dichloroethane and/or burnt in the burning process. Carbon dioxide obtained from synthesis of acetone is used in the process of producing carbonic acid.

EFFECT: wide range of obtained finished products and prevention of formation of industrial wastes.

4 cl, 1 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: method of producing cumene includes interaction of benzene with acetone and hydrogen with catalytic compound added as containing one or more zeolite in acid form or preferentially acid form, copper and, optionally, one or more element chosen from elements of groups IIIA, VIB, VIIB. Additionally the given invention concerns method of producing phenol with using cumene prepared by the method as described, catalytic compound for production cumene, and also methods of producing catalytic compound for cumene.

EFFECT: application of the methods and catalytic compounds specified above allows simplifying considerably producing phenol from cumene, allowing for simultaneous one-stage reaction for all chemical transformations required to produce high-yield cumene from acetone, benzene and hydrogen with minimum amount of secondary reactions of various reagents, intermediate compounds and products.

69 cl, 16 ex, 2 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: one of method versions is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification and possibly partial recycling into reaction zone(s) of one or several components of reaction mixture. Decomposition is carried out in presence of inert easily-boiling solvent, which contains mainly hydrocarbons, whose boiling temperature is lower than 70°C, preferably lower than 40°C, but not lower than minus 1°C, which is partially evaporated directly from reaction zone(s) and partially distilled from obtained reaction mixture, is in liquid state returned to reaction zone(s) with supporting in it (them) temperature from 1 to 70°C, preferably from 10 to 45°C. Second method version is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification. Applied is easily-boiling solvent, which after separation from reaction mixture, possibly with part of ketone, is recycled into reaction zone(s), and sulfocationite catalyst in H+ form, resistant in liquid media, containing alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons in large amount, at temperatures up to 70°C, in fine-grain or coarse-grain form, possibly, in form of mass-exchange filling with size from 1.5 to 25 mm.

EFFECT: obtaining phenol and ketones without formation of large amount of by-products and resins and practically without equipment corrosion.

14 cl, 1 dwg, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a single-step method of producing acetaldehyde via oxidation of ethylene in the presence of aqueous catalyst solution consisting of copper chloride and palladium chloride solution, while maintaining circulation of the aqueous catalyst solution in a reactor with a recirculating loop consisting of a reactor and a fog trap, characterised by that the entire outer wall of the reactor with a recirculation loop is heat insulated and its part which is under pressure is made from material which is resistant to corrosion by the aqueous catalyst solution or from ordinary material which is not resistant to corrosion by the aqueous catalyst solution, wherein the inner wall of the reactor is coated with corrosion-stable material having sufficient thermal stability at reaction temperature.

EFFECT: use of the present method improves volume-time-output factors, thereby increasing efficiency of the apparatus.

7 cl, 1 dwg

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