Method of production of phenols

FIELD: chemical industry; methods of production of the phenols by the catalytic decomposition of the cumene hydroperoxide into phenol and acetone.

SUBSTANCE: the invention is pertaining to production of phenols by the catalytic decomposition of the cumene hydroperoxide into phenol and acetone. The method provides for oxidization of the cumene into the cumene hydroperoxide, catalyzed by the acid decomposition of the cumene hydroperoxide, neutralization of the produced product of the decomposition, maintaining the product in the homogeneous phase before neutralization, which is conducted by means of the aqueous base. The phenol is separated by fractionation of the neutralized product. The aqueous base represents the water solution of the sodium hydroxide or phenoxide. In particular use the regenerated phenoxide, at least, on one phase of the treatment at production of the phenol. It is preferential to add the sodium hydroxide water solution to the reaction product in such a concentration and such amount, that to receive the concentration of sodium phenolate in the homogeneous phase from 0.2 up to 2.5 mass %. The temperature of the homogeneous phase after the add-on of the aqueous base is set within the range of 20°С-150°С, the preferable temperature is within the range of 60°С-120°С. It is preferential, that the reaction product is saturated with the oxygen-containing gas. The technical result of the invention is the decreased quantity of the undesirable impurities in the products of the acid decomposition of the cumene hydroperoxide.

EFFECT: the invention ensures the decreased quantity of the undesirable impurities in the products of the acid decomposition of the cumene hydroperoxide.

13 cl, 4 ex

 

The present invention relates to an improved process for the preparation of phenols.

The way acid-catalyzed cleavage of cumene hydroperoxide to phenol and acetone is particularly great industrial importance for a long time. Upon receipt of phenol from cumene by way of Hawkeye the cumene is oxidized to cumene hydroperoxide (CAS) for the first reaction stage, known as oxidation, and CAS consistently concentrated to a concentration of from 65 to 90 wt.% by vacuum distillation, known as concentration. In the second reaction stage, known as splitting, CSE is cleaved to phenol and acetone by the action of acid, usually sulfuric acid. At this stage dimethylphenylcarbinol (DMPC), formed during the oxidation, partially split in the equilibrium reaction to α-methylsterol (AMC) and water, while the other part DMFC reacts with PCG education dicumylperoxide (DCT); the rest remains in the product splitting. After neutralization product of the splitting of the specified mix products are usually processed through distillation.

The splitting part of the AMC or DMFC forms a high-boiling products (dimers, cumylphenol, bisphenola), which are discharged as residue in the distillation. AMC still present after neutralization, distillation hydrogenized is in the cumene and returned to the oxidation. DMFC, which is not reacted in the decomposition, ultimately remains in the form of a high-boiling component in the residue; part of it reacts further in the columns with hot phenol with the formation of AMC, which again formed the high-boiling secondary components. DCT is stable under normal temperatures splitting (50-70°). It decomposes thermally in columns with hot phenol, forming, on the basis of our experiments, o-cresol, at least partially. On the other hand, in the presence of acid DCT can be split into phenol, acetone and AMS at temperatures above 80°C. it is Therefore evident that the remaining DMPC and DCT, resulting in the cleavage, directly after cleavage will react completely due to the increase of temperature in the presence of acid used as a catalyst in the decomposition. Thus, DMPK largely turned into AMS and DCT becomes virtually entirely in phenol, acetone and similarly in AMS.

This additional thermal treatment of the cleavage product is already described in U.S. patent US 2757209, where we used a temperature above 100°specifically from 110 to 120°C. the Purpose of this additional thermal processing was complete dehydration DMFC in AMS. On the other hand, in U.S. patent US 4358618 describes heat addition is sustained fashion processing, which aims to transform DCT, resulting in the splitting, phenol, acetone and AMS; in this patent is used a temperature of 120 and 150°C. In U.S. patent US 5254751 describes additional thermal processing, which has the same purpose as in the US 4358618, and there are temperature from 80 to 110°C. finally, in the German patent application DE 19755026 A1 additional processing is carried out in the temperature range above 150°C. In all these processes, known from previous technologies, thermally treated product is successively cooled to (usually) 40°using the refrigerator, then neutralized and after separation of the salt containing aqueous phase is treated by distillation.

The disadvantage of the above methods is that hydroxyacetone and other carbonyl compounds such as acetaldehyde, propionic aldehyde and phenylpropanal, are formed as by-products and these products, first of all, hamper the processing of the reaction products and, secondly, hydroxyacetone partially reacts with phenol in the specific processes of purification of phenol with the formation of high-boiling products, thus leading to undesirable losses of phenol. It would therefore be desirable to reduce the content of hydroxyacetone and other impurities in the product splitting.

In U.S. patent US 606667 describes how to remove hydroxyacetone and other carbonyl compounds from the product of the cleavage of cumene hydroperoxide. For this purpose, the reaction product of the cleavage of cumene hydroperoxide is extracted with aqueous salt solution in the temperature range 15-80°With removal of hydroxyacetone, among other things. Downloaded extractant (extracting phase) is then processed in a separate reactor, in order to make hydroxyacetone in the condensation products. Extractant, which was thus treated, returned to the stage extraction, where the condensation products are sent in the organic phase is then separated in the processing of phenol and acetonaemia the organic phase. The examples show that, despite the very sophisticated equipment used for cleaning extraction, and subsequent reaction extracted hydroxyacetone phase with an organic product, which is supplied to further processing for separation of phenol, still contains 500-800 ppm of hydroxyacetone.

In addition, it was found that sodium hydroxide, is still present in extractant, will react with the phenol present in the organic phase product splitting, when extractant returned to the stage extraction. The power base of sodium phenolate formed is too low, in order to achieve a noticeable speed reactions of hydroxyacetone in the aqueous phase after e is straccia. In addition, in the process illustrated in U.S. patent US 6066767, be sure to add fresh sodium hydroxide at a stage where hydroxyacetone turns into a high-boiling products. Thus, an additional disadvantage of the process disclosed in US 6066767, is that fresh source material, like sodium hydroxide, is used and largely goes to waste, leading to unnecessarily high production costs for the described process.

In the work Vasilyeva I.I. and others, "oil Refining and Petrochemical industry", Moscow, Russia (2000), (12), 34-38, the process of extraction and transformation of hydroxyacetone from the product of the cleavage of cumene hydroperoxide similar set forth in U.S. patent US 6066767. The only open addition to the material listed in the US 6066767, is that air can be introduced into the reactor, where water extracting phase, including hydroxyacetone, is treated by adding sodium hydroxide, to increase the rate of conversion of hydroxyacetone. Therefore, the process described Vasilyeva, etc. has the same weaknesses as the process known from US 6066767.

Of bids US US 2002-0183563 known method for production of phenol, in which the pH of the reaction product from the acid catalyzed cleavage alkylaryl-hydroperoxides ustanavlivat the SJ when the value at least 8 by adding a basic aqueous solution at a temperature of at least 100°before processing the product. Therefore, the primary emulsion of an aqueous solution in the organic phase of the cleavage product is formed in such a way that the result is supposed to be processed a large volume flow of inhomogeneous two-phase mixture, just as for the process in the US 6066767. In addition, it was shown that under the reaction conditions described in US 2002-0183563 formed condensation products with acetone, resulting in a loss of the target product.

In U.S. patent US 4283568 describes the process of regeneration of phenol from the reaction mixture obtained from the acid cleavage of cumene hydroperoxide. Neutralization of the acid reaction mixture is an aqueous solution of sodium phenolate, which enters the recirculation flow at the subsequent stages of the treatment process. The number of added aqueous solution is such that there is formed a heterogeneous two-phase mixture and the aqueous phase must be separated from the organic phase in the separator.

In the process described in U.S. patent US 3692845, non-aqueous component, comprising polyamine connection is added to the phenol obtained by acid cleavage of cumene hydroperoxide, in order to uninstall the related carbonyl impurities.

Therefore, the object of the invention I have is to provide a method of obtaining phenols, in which reducing the number of undesirable impurities, primarily hydroxyacetone, before processing the product can be achieved in a simple way without the loss of valuable products.

This goal is achieved by using a method of producing phenol by adding an aqueous base to the reaction product of the acid catalyzed product splitting alkaloidshenobarbital while maintaining a homogeneous phase before handling product.

Surprisingly it was found that this simple procedure leads to a significant decrease in the content of undesirable by-products, in particular hydroxyacetone, without complex equipment described in the previous technology, cited by necessity. In addition, it was found that the rate of conversion of undesirable by-products in high-boiling compounds which can be easily separated at the subsequent stages of processing, much higher even at low temperatures if the reaction product obtained from the acid cleavage of alkaloidshenobarbital, is held in a homogeneous phase. It is also remarkable that the overall selectivity of the process will not be compromised by the addition of an aqueous base in a homogeneous phase, i.e. the reaction using target products after adding water Foundation in homogeneous phase is insignificant. the moreover, an additional advantage of the present invention is that adding to hydroxyacetone other undesirable carbonyl functional by-products like aldehydes, mainly acetaldehyde, propionic aldehyde and phenylpropionic aldehyde, at the subsequent stages of processing, leading to loss of the target product or creating problems in the separation of the desired products can be transformed into a high-boiling compounds which can be easily separated without reducing the total output of the target product.

A further advantage, in comparison with the previous technology where or organic phase of the reaction product obtained from the cleavage alkylaryl-hydroperoxide, extracted aqueous phase to remove hydroxyacetone, or adding a base leads to the fact that in heterogeneous phase, the total amount of threads participating in the process according to the present invention, is reduced as the aqueous base is added to the reaction product only in the space in which there is a homogeneous phase. Thus, the production and investment costs for the process of the present invention are significantly reduced, while improving the separation of undesirable side products.

According to a preferred form of execution this is about the invention of the aqueous base is selected from solutions of aqueous sodium hydroxide and water phenoxide, when this aqueous solution of peroxide especially preferred. If added to an aqueous solution of sodium hydroxide, then this leads to an increase in the concentration of peroxide in homogeneous phase. If in the process of the present invention are aqueous solutions of peroxide, an aqueous solution of peroxide, regenerated, at least one processing stage of the process of obtaining phenols, can be advantageously used for the production of phenol.

In contrast to previous processes technology, where the transformation of by-products, such hydroxyacetone, is carried out in the aqueous phase and therefore the addition of fresh sodium hydroxide is required, the method of the present invention allows the use of threads of the process of regeneration. Especially preferred if the base catalyzed the transformation of the carbonyl functional group a by-product, such hydroxyacetone, is carried out in accordance with the present invention in a homogeneous organic phase, the power base of phenoxide is sufficient in order to achieve sufficient velocity transformation. Thus, the method of the present invention has a very significant economic advantage over previous technological processes do not require the addition of fresh sodium hydroxide.

Preferably, Fe is the oxide is a phenolate sodium, and an aqueous solution of sodium phenolate or an aqueous solution of sodium hydroxide is added to the reaction product in such concentration and of such amount to obtain a concentration of sodium phenolate in a homogeneous phase from 0.2 to 2.5 wt.%, preferably the concentration of sodium phenolate in homogeneous phase is from 0.5 to 1 wt.%.

The concentration of the basic compound in a homogeneous phase reaction product and water base is given by the number and concentration of the aqueous base is added to the reaction product. The only restriction is that after you add the base mix base and the reaction product was still homogeneous. It is particularly important that the amount of water introduced with the addition of an aqueous base, must not exceed the limit of solubility in the reaction product. The solubility of water in the reaction product will depend on the concentration of each component present in the reaction product. Thus, the limit of solubility can vary widely, but usually lies within the range of 5-12 wt.%. Experienced expert engineer may determine the solubility of water in the reaction product specific phenolic process standard methods and can easily set the amount and concentration of the aqueous base that you want to add the TB without additional experiment, in order to satisfy the requirement of this process is that the reaction product was kept in a homogeneous phase.

As noted above, in the method of the present invention the temperature is less critical, such as in the method described in the German patent application DE 10110392. Thus, in this process the temperature of the homogeneous phase can be installed in a wide range of 20-150°C, preferably 60 to 120°S, most preferably from 80°C to less than 100°C.

According to a particularly preferred form of execution of the present invention the oxygen-containing gas is introduced into the reaction product. Thus the rate of conversion of carbonyl functional undesirable side product can be greatly increased. Therefore, the temperature and/or time of exposure in the treatment of the reaction product can be reduced. Thus production and investment costs of this method can be significantly reduced.

Although Vasiliev I.I. and others have already established that the introduction of air, the rate of conversion of hydroxyacetone can be increased, this fact clearly limits the introduction of air into the aqueous phase, containing hydroxyacetone, after the aqueous phase separated from the organic phase of the product. Thus, in the method described Vasilyeva the other, the cleavage product does not come into contact with oxygen. Not wishing to be bound by theory, it is assumed, especially when interpreting work Vasilyeva, etc. that oxygen will oxidize hydroxyacetone, thereby increasing the speed and efficiency of conversion of hydroxyacetone. Therefore, we should expect that, if oxygen-containing gases come into contact with the product splitting, which according Vasilyeva I.I., etc. should be strictly avoided, it is valuable products will be similar to disintegrate due to oxidation reactions, resulting in the total loss of selectivity and exit.

But the authors of the present invention surprisingly found, in contrast to the above expectations that the introduction of oxygen in homogeneous phase reaction product and water base does not lead to a noticeable splitting of valuable products, despite the fact that valuable then the products will be in contact with oxygen. Thus, surprisingly, the introduction of oxygen in homogeneous phase reaction product does not impact adversely on the selectivity of the overall process.

To achieve the desired effect of increasing the rate of conversion of hydroxyacetone the amount of oxygen introduced in a homogeneous phase, must comply with at least the stoichiometric quantity of rootstudio of hydroxyacetone. Normally used in excess relative to the stoichiometric quantity. According to a preferred form of execution of the present invention, a homogeneous phase reaction product and water base saturated oxygen-containing gas. If the amount of the oxygen-containing gas exceeds the saturation limit, to form a continuous liquid phase with the gas bubbles, dispergirovannykh it. Preferably the oxygen-containing gas may be fed under pressure. A suitable pressure is in the range from 1 to 10 barabs.

Preferably the oxygen-containing gas is selected from oxygen and air. The advantage of using oxygen, especially when there is a saturation of a homogeneous phase with oxygen, is that not formed a separate gas phase, which should be removed from the system in a separate purged gas stream.

The method according to the invention with particular advantage may be combined in known processes for the production of phenol by the following General stages:

a) acid catalyzed cleavage of alkaloidshenobarbital and

b) subsequent thermal treatment of the cleavage product from stage a), at a temperature of stage (b), which is higher than in stage a),

because here is the reaction product of cleavage of alkylarylsulfonate mainly the zoom is obtained at a temperature at least 100°C. Therefore, the reaction product already has the desired temperature necessary for the process according to the present invention, or may be cooled to the desired temperature. In any case, there is no need for additional energy for heating.

The method according to the invention is suitable for acid catalyzed cleavage of one or more alkaloidshenobarbital (AGP), for example, cumene hydroperoxide, α-methylbenzol, cumene hydroperoxide, α-methyl-p-methylbenzyl, cumene hydroperoxide, α,α-dimethylbenzyl, also known as of cumene hydroperoxide or cumene hydroperoxide (CHP), hydroperoxide α,α-methylethylbenzene, also known as the hydroperoxide second-butylbenzene, cumene hydroperoxide, α,α-dimethyl-p-methylbenzyl, cumene α,α-dimethyl-p-ethylbenzene, cumene hydroperoxide, α-methylα-phenylbenzyl. The method according to the invention are particularly used for the acid catalyzed cleavage of a mixture of alkaloidshenobarbital, including at least cumene hydroperoxide (CAS). The method according to the invention is particularly preferably used for splitting KGP.

Further, the method according to the invention will be described using an example for the case of the acid catalyzed cleavage of CSB to phenol and acetone, without restricting the method according to the image the structure of this form of execution.

As a catalyst for splitting KGP preferably used sulfuric acid. The mixture of cleavage products preferably has a sulfuric acid concentration of 50 to 1000 ppm (mass.). It may be advantageous to modify the activity of the acid, i.e. the strength of the acid cleavage products, before heat treatment. The strength of the acid depends on the acid concentration and the water concentration in the mixture after splitting. The higher the water content in the mixture after cleavage, the more acid must be added to the mixture splitting, in order to obtain the same activity of the acid, while the acid strength is inversely proportional to the square of the concentration of water. Thus, for example, the acid strength of the solution mixture splitting, containing 200 ppm (mass.) sulfuric acid and 2% by weight of water, is only one-sixteenth of the strength of the acid solution mixture splitting, containing 200 ppm (mass.) sulfuric acid and 0.5% by weight of water.

The ideal strength (concentration) acid and thus the ideal mixture splitting in relation to the acid concentration and the water concentration can be determined by simple preliminary tests. In the case of a mixture splitting, having a water concentration up to 6% by weight, sulfuric acid concentration of 100 to 500 ppm (mass.) in a mixture splitting, as it was found, is especially ugodnoy. In order to increase the strength of the acid, usually add additional sulfuric acid. In order to reduce the concentration of acid can be added to the product of cleavage of a base, for example, a solution of peroxide ammonium or sodium hydroxide solution or water. Preference is given to adding water to the product of cleavage.

In a particularly preferred form of execution of the method of the invention, the cleavage product, thermally processed, has a concentration of CAS, which in combination with the concentrations of other compounds, reacting exothermically during the cleavage reaction, it releases the same amount of heat that will heat the mixture of fission products to the desired temperature for the subsequent thermal processing.

All forms of execution described in the German patent application DE-A 10021482, and suitable reactors can be similarly used in the method of the present invention. Alternatively, you can also use procedures similar to those described in emetsky the patent application DE-A 10051581, in order to obtain the mixture of cleavage products from step a) and a concentrate comprising at least cumene hydroperoxide, divide this mixture of at least two parts and apply at least one of these parts in acid catalyzed Rasse is of the stage a), and the other part be subjected to a subsequent thermal treatment according to stage b) and set the pH of the reaction product from stage b) in accordance with the invention.

At least two parts of the mixture preferably processed in such a way that one part is processed at a temperature of from 45 to 99°C, preferably from 45 to 90°With, in order to cause the cleavage of cumene hydroperoxide, and the other part is heated to a temperature above 100°so that happened cleavage of cumene hydroperoxide. As for the part which is heated to temperatures above 100°C, cleavage of cumene hydroperoxide takes place together with the joint subsequent thermal processing. This part is preferably processed at temperatures above 115°S, especially preferably above 130°and in the highest degree, preferably above 150°and return with this temperature of the exothermic reaction at this stage.

The exact composition of the mixture which is subjected to high temperature decomposition or thermal post-processing, in order to obtain the desired temperature, is described in detail in the German patent application DE-A 10051581. Related to this problem the patent disclosure publication thus included here by reference. In addition, all options, op the sledge in the German patent application DE-A 10051581, and suitable reactors can also be used in the process of the present invention.

Assume without recourse to theory that hydroxyacetone and other carbonyl functional by-products formed in the cleavage reaction, according to the invention react, due to the presence of a basic compound in a homogeneous phase, with the formation of the condensation products and/or, if present oxygen, oxidation products, which can be easily separated from the mixture of products. In addition, there is a suppression of acid catalyzed secondary reactions, including the reaction of hydroxyacetone with phenol, which leads to loss of yield of phenol and may continue during the cooling phase. Thus, the method according to the invention leads as to the simplified removal of by-products and to improve the selectivity, as hydroxyacetone is removed through reaction of the products of cleavage, and at the same time undesirable reaction hydroxyacetone with phenol, among other things, is suppressed.

In order to carry out the method according to the invention, first of all, remove hydroxyacetone and other by-products of fission products due to the reaction by-products with the formation of the condensation products, which can be controlled more easily, can also be useful in is the input of the cleavage product in the vessel for temporary stay after adding water the grounds and before cooling. Depending on the selected temperature, the duration of stay may be set in the range 10-7200 seconds, preferably 10-3600 seconds, the residence time decreases with increasing temperature of the products of cleavage.

The method according to the invention allows to obtain a mixture comprising phenol and acetone, in which the content of hydroxyacetone does not exceed 400 ppm (mass.), preferably 300 ppm (mass.), particularly preferably 200 ppm (mass.) and highly preferably 100 ppm (mass.).

In subsequent process operations after processing according to the present invention, the cleavage product, if necessary, cooled, then neutralized and fractionized. These stages are known qualified professional technicians, and are not critical to the present invention, so that a more accurate description is not necessary.

Operational (working) characteristics of the method of the invention are illustrated by the following examples.

Comparative example 1:

The cleavage product was obtained from cumene hydroperoxide 70%concentration by weight. The cleavage product was cooled to 40°and then neutralized (pH=7). The cleavage product consisted of 42 wt.% phenol, 26 wt.% acetone, 3.1 wt.% alpha-methylstyrene and 1200 ppm (mass.) hydroxyacetone, in addition to other organic comp is required. All concentrations refer to the total amount of organic components (anhydrous). In addition, attended 1 wt.% water.

Comparative example 2:

The cleavage product of comparative example 1 was mixed with 1.5%aqueous solution of sodium phenolate (42%phenolate sodium) and water in an amount required to obtain a biphasic mixture of 90% by volume of the organic phase and 10% by volume of the aqueous phase. The pH value of the aqueous phase was approximately 10,5. Two phases were intensively mixed at 120°C for 2 hours. The cleavage product consisted of 42 wt.% phenol, 26 wt.% acetone, 3.1 wt.% alpha-methylstyrene and 755 ppm (mass.) hydroxyacetone, in addition to other organic components. All concentrations refer to the total amount of organic components (anhydrous).

Example 1

Comparative example 1 was repeated with the difference that the cleavage product was dissolved 1.0 wt.% the sodium phenolate. Phenolate sodium was added with 42% (by weight) aqueous solution of sodium phenolate, and the water content in the product of cleavage was increased to 2.4 wt.%. The mixture of fission products and the aqueous phenolate solution remained homogeneous. Homogeneous mixture was saturated by air, by introducing air under pressure 3 barabs. The mixture was stirred for 2 hours at 80°at constant pressure of air. Product rossalini is consisted of 42 wt.% phenol, 26 wt.% acetone, 3.1 wt.% alpha-methylstyrene and 300 ppm (mass.) hydroxyacetone. All concentrations refer to the total amount of organic components (anhydrous).

Example 2

Comparative example 1 was repeated with the difference that the cleavage product was dissolved 1.5 wt.% the phenolate sodium, with water content in the product of cleavage was increased to 2.4 wt.% Phenolate sodium was added with 42% (by weight) aqueous solution of phenolate, and the water content in the product of cleavage was increased to 3.1 wt.%. The mixture of fission products and the aqueous phenolate solution remained homogeneous. Homogeneous mixture was saturated by air, by introducing air under pressure 5 barabs. The mixture was stirred for 2 hours at 80°at constant pressure of air. The cleavage product consisted of 42 wt.% phenol, 26 wt.% acetone, 3.1 wt.% alpha-methylstyrene and less than 50 ppm (mass.) hydroxyacetone. All concentrations refer to the total amount of organic components (anhydrous).

When comparing the examples of the present invention with the comparative examples it is evident that the content of hydroxyacetone can be significantly reduced without reducing the selectivity and yield of the target products of phenol, acetone and alpha-methylstyrene.

1. Method for production of phenol, involving the oxidation of cumene hydroperoxide in which umala, acid catalyzed cleavage of cumene hydroperoxide and processing of the obtained product splitting involving the neutralization of the resulting product of the cleavage and subsequent fractionation of the resulting product to highlight phenol, wherein the aqueous base is added to the reaction product from the acid catalyzed cleavage while maintaining a homogeneous phase before neutralization and fractionation of the product.

2. The method according to claim 1, where the aqueous base is selected from water solutions of sodium hydroxide and water phenoxide.

3. The method according to claim 2, where the base is an aqueous solution of peroxide, regenerated, at least one processing stage process for production of phenol.

4. The method according to claim 2, where phenoxide is a phenolate sodium, and an aqueous solution of sodium phenolate or an aqueous solution of sodium hydroxide is added to the reaction product in such concentration and of such amount to obtain a concentration of sodium phenolate in a homogeneous phase from 0.2 to 2.5 wt.%.

5. The method according to claim 4, where the concentration of sodium phenolate in homogeneous phase is from 0.5 to 1 wt.%.

6. The method according to claim 1, where the temperature of the homogeneous phase is set after adding aqueous base in the range of 20-150°C, preferably 60 to 120°S, most preferably from 80 to which the Eney than 100° C.

7. The method according to claim 1, where the oxygen-containing gas is injected into the reaction product.

8. The method according to claim 7, where the reaction product is saturated with oxygen-containing gas.

9. The method according to claim 7, where the oxygen-containing gas is injected under pressure.

10. The method according to claim 7, where the oxygen-containing gas selected from oxygen and air.

11. The method according to claim 1, wherein prior to processing the product homogeneous phase comprising the reaction product and water base support in a vessel for temporary stay.

12. The method according to claim 11, where the residence time is 10-7200 C.

13. The method according to any of the preceding paragraphs, in which the reaction product is cooled prior to neutralization of the reaction product.



 

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5 cl, 3 dwg, 6 tbl, 4 ex

FIELD: organic chemistry, medicine, pharmacy.

SUBSTANCE: invention relates to new derivatives of glucopyranosyloxybenzylbenzene represented by the formula (I): wherein R1 represents hydrogen atom or hydroxy(lower)alkyl; R2 represents lower alkyl group, lower alkoxy-group and lower alkylthio-group being each group is substituted optionally with hydroxy- or (lower)alkoxy-group, or to its pharmaceutically acceptable salts. Also, invention relates to pharmaceutical composition eliciting hypoglycemic activity and to a method for treatment and prophylaxis of hyperglycemia-associated diseases, such as diabetes mellitus, obesity and others, and to their intermediate compounds. Invention provides preparing new derivatives of glucopyranosyloxybenzylbenzene that elicit the excellent inhibitory activity with respect to human SGLT2.

EFFECT: valuable medicinal properties of compounds.

13 cl, 2 tbl, 2 ex

The invention relates to petrochemistry and can be used in the production of phenol and acetone Kukolnik method

The invention relates to analytical chemistry of organic compounds and can be used for concentration of phenol in analytical control of natural water, drinking water and treated wastewater

The invention relates to a process for the production of phenol method Kukolnik

The invention relates to analytical chemistry of organic compounds and can be used for concentration of 2-naphthol in analytical control of treated wastewater enterprises producing and applying synthetic dyes
The invention relates to petrochemistry and can be used in the production of phenol and acetone Kukolnik method

The invention relates to petrochemical technology, namely the production of phenol and acetone Kukolnik method

The invention relates to chemical technology and can be used in the production of pyrocatechin and hydroquinone, which are widely used as intermediates for the production of antioxidants, pharmaceuticals, dyes, etc

FIELD: chemical industry; methods of extraction of phenol and biphenols from the homogeneous reactionary mixtures.

SUBSTANCE: the invention is pertaining to the method of extraction of phenol and biphenols from the homogeneous reactionary mixtures of the direct oxidation of benzene by hydrogen peroxide. The method includes delivery of the reactionary mixture containing benzene, water, phenol, the sulfolane and the reaction by-products (biphenols) in еру distillation plant consisting of two or more columns for production of one or more products basically consisting of the azeotropic mixture of benzene with water and phenol, and also the product consisting of sulfolane, phenol and the reaction by-products. The stream including sulfolane is mixed with the water solution of the base and benzene for formation of the salts of the phenols and the subsequent stratification of the mixture, extraction by benzene and separation in the flow column containing benzene and sulfolane, which is returned in the reactor. From the same column separate the stream including sodium phenolates in the water solution, which is treated with the sulfuric acid for extraction of the phenols from their salts. At the stage of the extraction separate the extracting solvent, after distillation of which in the tailings bottom product receive the biphenols water solution. The separated organic solvent recirculates in the system. The technical result of the invention is improvement of the process of separation of phenols and biphenols from the complex azeotropic mixtures containing sulfolane.

EFFECT: the invention ensures the improved process of separation of phenols and biphenols from the complex azeotropic mixtures containing sulfolane.

9 cl, 1 ex, 1 dwg, 1 tbl

The invention relates to the synthesis of organic compounds, particularly to the technology of producing bisphenols, and can be used in the chemical industry for the production of monomers, antioxidants and biologically active substances

FIELD: industrial organic synthesis.

SUBSTANCE: isopropyl alcohol production process comprises hydrogenation of starting acetone including from 0.01 to 10000 ppm benzene in presence of hydrogen and catalyst to give isopropyl alcohol and benzene hydrogenation products, acetone and benzene contained in feedstock being hydrogenated simultaneously. In its second embodiment, isopropyl alcohol production process comprises product separation stage. Process of producing phenol and isopropyl alcohol containing benzene hydrogenation products comprises stages: alkylation of benzene with isopropyl alcohol and/or propylene to form cumene, oxidation of resulting cumene into cumene hydroperoxide, acid cleavage of cumene hydroperoxide to produce phenol and acetone including from 0.01 to 10000 ppm benzene, preferably concentration of produced benzene-polluted acetone, and catalytic hydrogenation of benzene-polluted acetone into isopropyl alcohol containing benzene hydrogenation products, hydrogenation of benzene and acetone proceeding simultaneously.

EFFECT: enhanced process efficiency.

3 cl, 1 dwg, 1 tbl

FIELD: chemical industry; methods of production of phenol and acetone.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the industrial process of production of phenol and acetone by the cumene method. The method is realized by decomposition of the technological cumene hydroperoxide in the in series connected reactors in two stages with formation on the first stage of the dicumylperoxide at the temperature of 40-65°С at presence as the catalytic agent of 0.003-0.015 mass % of the sulfuric acid with its subsequent decomposition on the second stage in the reaction medium at the temperature of 90-140°С. The process is conducted at the excess of phenol in the reaction mixture at the molar ratio of phenol : acetone exceeding 1, preferentially - from 1.01 up to 5. Excess of phenol is formed either by distillation (blowing) of acetone or addition of phenol in the reaction medium. The technical result of the invention is reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

EFFECT: the invention ensures reduction of formation of hydroxyacetone, which one worsens the quality of the commercial phenol.

5 cl, 4 ex, 8 tbl

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of compounds of oxirane, phenol and ketones and/or aldehydes. Proposed method involves the following steps: (i) oxidation of alkylaryl wherein alkyl substitute comprises from 2 to 10 carbon atoms to yield alkylaryl hydroperoxide; (ii) contacting at least part of alkylaryl hydroperoxide prepared at the step (i) with olefin in the presence of catalyst to yield oxirane compound and alkylaryl hydroxyl; (iii) reaction of at least part of alkylaryl hydroperoxide prepared at the step (i) to yield phenol and ketone and/or aldehyde; (iv) separation of oxirane compound from the reaction product from the step (ii), and (v) contacting at least part of the reaction product no containing oxirane with hydrogen to yield alkylaryl and at least part of the latter is re-circulated to the step (i). Invention provides the development of the combined method for synthesis of oxirane, phenol, ketones and/or aldehydes that allows reducing the amount of by-side products due to their conversion to useful compounds.

EFFECT: improved method of synthesis.

8 cl

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