crude acetone which is obtained in the acid-catalyzed cleavage of cumene hydroperoxide. The process of the invention for preparing phenol from benzene comprises the four process steps. However, the phases obtained can also be passed to a distillation in which the various compounds are removed from the phases. All subreactions are favored or accelerated by the presence of the ß zeolite catalyst. generation, Method for manufacturing maltose-rich products, Process for the Monosulfonation of Aromatic Phosphines, and Zwitterionic Product Derived Therefrom, Process for Production of Substituted Cyclopentanone, USE OF alpha,beta -UNSATURATED CARBONYL COMPOUNDS AS QUENCH REAGENTS FOR THE BIRCH REDUCTION, Process for preparing ruthenium-carrying alumina and process for oxidizing alcohol, Process for Synthesis of (3S)- and (3R)-3-Hydroxy-Beta-Ionone, and Their Transformation to Zeaxanthin and Beta-Cryptoxanthin, Method for heating and cooling using fluoroether compounds, compositions suitable therefore and their use, Methods for making(-)-menthol and oxygenated menthane compounds, METHODS OF USING TUNGSTEN CARBIDE CATALYSTS IN PREPARATION OF ETHYLENE GLYCOL. According to the invention, isopropanol is dehydrated to propene in the liquid phase in the presence of the catalyst of the present invention and at the same time benzene is alkylated by means of isopropanol to form cumene. This can be ensured, for example when using a trickle-bed reactor, by using high linear velocities of the liquid phases in the reactor, preferably greater than 30 m/h. in a phase separator. 2, consists of tube A in which there is an inlet of the acid component (1) and an inlet, upstream of this, of CHP (2) and acetone (3). The aqueous phase can be worked up or disposed of. Be the first to rate this post. The n-propylbenzene content of the reaction mixture or reactor output is usually less than 300 wppm, preferably less than 150 wppm, when carrying out the process of the invention. The process of claim 14, wherein the acetone used is crude acetone. Preference is given to adding an acid catalyst to the reaction mixture in such an amount that the content of acid catalyst is from 0.002 to 5% by weight. The acid-catalyzed cleavage of cumene hydroperoxide is described, for example, in. Preference is given to separating the reaction mixture obtained from the reactor into an organic phase and an aqueous phase in a liquid/liquid phase separator like a decanter prior to distillation, in which case it can be advantageous to remove part of the heat energy from the reaction mixture before it enters the phase separator, e.g. It was invented by R. Ūdris and P. Sergeyev in 1942 (USSR). For the production of isopropanol ethers, combination processes involving hydrogenation and etherification are usually employed. The acidity of the catalyst is modified by the water formed in the reaction. The addition of the alkaline compound to the cumene-containing solution is preferably carried out so that the pH of the cumene-containing solution does not go outside the pH range from 2 to 11 even as the reaction progresses. Die Oxydationsgechwindigkeiten und Ausbeuten von in einem Pyrex-Reaktor bei 110–130°C durchgeführten Versuchen werden erwähnt. A person skilled in the art of phenol production will be able to see further possible combinations which are likewise subject matter of the present invention. Upon further treatment of cumene hydroperoxide with dilute acid, we get the phenols. 1. The oxidation of the cumene to cumene hydroperoxide is preferably carried out continuously. The concentration of CHP, to values higher than 70% by weight, takes place by evaporation/distillation in specific equipment. The process of any of the preceding claims, wherein the water content of the total feed stream to the reactor does not exceed 5 wt.-% based on the weight of the total feed stream. All rights reserved. Propene is generated in the reactor by the simultaneous isopropanol dehydration. —COOH of ketones, Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. In the various process stages, different temperature and/or pressure conditions can be employed. As is known, phenol can be produced from cumene. Published by Elsevier Ltd. All rights reserved. A description is given of an apparatus for continuous preparation of phenol from cumene and a simplified flow sheet for production on a larger scale is added. The distributor is positioned at the base of the reactor and allows the air fed to flow upwards, touching the walls of the mantle, in the form of bubbles. To hydrogenate acetone which has not been reacted in the first process stage, the reaction mixture from the circulation reactor is passed to a tube reactor. appropriate extrudates, of the catalyst used. Finally, a proton is lost from the protonated acetone molecule, leading to the formation of acetone. from your Reading List will also remove any The bottoms were passed to thermal utilization. The cleavage product mixture, which can come directly from the cleavage reactor or else from the subsequent heat treatment, is worked up by distillation. This can be achieved by high linear velocities. Process for the alkylation of aromatic compounds. versalis S.p.A. (San Donato Milanese (MI), IT), OBLON, MCCLELLAND, MAIER & NEUSTADT, L.L.P. The present invention relates to a process for the preparation of phenol from cumene. a second substantially cylindrical structure (downcomer), open at the ends (bases), inside and coaxial with the first structure; and. The feedings of the whole of the acid (10) and part of the CHP (11) and acetone (12) respectively, are present in the tube of the system (70). The two exchangers, arranged in the cycle, are connected to each other so that the outlet of one becomes the feeding of the other, and vice versa. Die scheinbare Aktivicrungsenergie der nichtkatalytischen Oxydation wurde zu 16 kcal/mol bestimmt. However, it can likewise be advantageous for the isopropanol from step IV to be purified by suitable measures, e.g. The ability to hydrogenate crude acetone directly makes it possible to omit complicated work-up or purification of crude acetone obtained, for example, in the cleavage of cumene hydroperoxide. The reaction mixture then rapidly passes in the tubes of a tube-bundle reactor (B), while the heat of reaction is removed with cooling water, fed and dischrged through (4) and (5), flowing on the shell side. s.parentNode.insertBefore(gcse, s); A process for the preparation of cumene by reacting isopropanol or a mixture of isopropanol and propene with benzene in a liquid phase in presence of a ß-zeolite catalyst having a SiO, The process of claim 1 , wherein the catalyst used is a ß-zeolite having an SiO. https://doi.org/10.1016/S0009-2509(54)80006-6. By continuing you agree to the use of cookies. The organic phase is fed to a distillation column in which cumene, by-products and starting materials are separated from one another. Bei 120°C wurde stündlich, mit einer Ausbeute von 05% etwa 11.0 Gew.% Kumolhydroperoxyd in der Flüssigkeit gebildet. b. If liquid acids are used, they are added to the reaction mixture comprising CHP. The apparent activation energy of the non-catalytic oxidation of cumene was determined at 16 kcal/mole. It may be advantageous to remove part of the heat energy from the organic part of the reaction mixture which is recycled to the reactor by means of a heat exchanger. It would therefore be desirable to find a way of producing phenol in which no coproduct is formed. 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You can also prepare small amounts of phenol by the peroxide oxidation of phenylboronic acid and the hydrolysis of diazonium salts. selective catalysts, Recycling of unreacted starting or intermediate materials, Council Of Scientific And Industrial Research, 미쓰이 가가쿠 가부시키가이샤, Council of Scientific and Industrial Research, AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR, LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT, FLEISCHER, ENGELS & PARTNER MBB, PATENTANWAELT, DE, Hydrogenation of cleavage effluents in phenol production, Process for the preparation of isopropanol, Process for the alkylation of aromatic compounds, Process for producing alkylated aromatic compound and process for producing phenol, Process for preparing an alkylated aromatic compound, Method for producing alkylated aromatic compound and method for producing phenol, Process for the production of iso-propanol by liquid phase hydrogenation, Process for producing alkylated aromatic compounds and process for producing phenol, Method for producing an alkylated aromatic compound and method for producing phenol, Method for producing alkylated aromatic compound, method for producing cumene, and method for producing phenol.

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