Method for production of phenol, acetone and-methylstyrene, a method of producing phenol

 

(57) Abstract:

Phenol, acetone and methylsterol get a decomposition product of cumene oxidation containing cumene hydroperoxide, cumene and dimethylphenylcarbinol, in the presence of sulfuric acid. The method involves the cleavage of cumene hydroperoxide in the reactor with back-mixing at 55-80oC obtaining-methylstyrene from dimethylphenylcarbinol with subsequent treatment of the resulting reaction mixture in the reactor with a piston flow, where support higher temperature. In the reactor a reverse mixing process leading to conversion of dimethylphenylcarbinol not more than 35%, then add acetone to the reaction mixture, after which it is directed into the reactor piston type. The water concentration in the reaction mixture is maintained within the range of 0.5 to 3.0 wt.%. For the production of phenol is used, the reaction mixture containing phenol, acetone, cumene, dimethylphenylcarbinol and dicumylperoxide, and phenol and acetone are present in equimolar amounts. The specified reaction mixture was added acetone in an amount of 1.15 to 1.8 times its original concentration, heated to 80-100oC, after which the mixture is fed into the reactor with reciprocating flow for dehydra is m, immediately cooled and neutralized to terminate the reaction. Increases the yield of target products. 2 C. and 14 C.p. f-crystals, 5 PL.

This invention relates to a method for producing a phenol, which is used as an intermediate product for the production of synthetic resins, agrochemicals, dyes, pharmaceuticals, etc.

Proposed various methods for producing phenol and one of the most frequently used methods is the way the cumene-phenol, in which the starting compound for the synthesis of phenol is cumene. In this way the cumene oxidized by oxygen or air to obtain cumene hydroperoxide (hereinafter designated as "MSE"), which is cleaved to phenol and acetone in the presence of acid catalyst, the Main products of the way the cumene-phenol is phenol and acetone. In addition, in the oxidation of cumene as a by-product formed dimethylphenylcarbinol (hereinafter referred to as DMFC"), DMPC then dehydration by acid cleavage of CSB and getting-methylsterol (hereinafter referred to as "MS") as a by-product, and-MS easy hereroense back to cumene, which is again suitable as source material. a-MS can be used in industry as mo the odes of phenol (which is one of the final products of the cleavage reaction PCG) a-MS and so on, for example, the reaction between a-MS and phenol to form cumylphenol and dimerization of a-MS with dimer formation methylstyrene. Another by-product of the cleavage reaction KGP is a very small number of hydroxyacetone (hereinafter referred to "HA"). HA it is difficult to separate from phenol by distillation, and it can degrade the phenol, if present in this otherwise pure final product. If phenol containing HA, get bisphenol a is formed colored product, which has a very low commercial price. Moreover, HA is soluble in water and has such a high COD load that it dissolves in the wastewater way the cumene-phenol making it necessary biological or other treatment of these waters.

Among these problems, adverse reactions, which reduce the outputs of phenol and a-MS, caused by the method of the acid cleavage KGP after diluting it with a solvent, for example acetone (see, for example, published examined patent Japan N 3875/1952 and 4619/1953), or the method of conducting the reaction in more than one stage (see, for example, U.S. patent 2 757 209 and the publication of the last examination of the Japan patent N 13464/1962). In accordance with references to the increased efficiency of contact between the acid catalyst and CAS. The second proposal, described in U.S. patent 2 757 209, is carrying out the cleavage reaction KGP in several stages, with the first stage reaction of the acid cleavage is carried out in mild conditions at a lower concentration of acid catalyst and a lower temperature than in conventional way of completing the reaction for the production of phenol and a-MS in one stage, so that the product remains a few percent of CSB; in the second stage of the reaction product of the first stage is introduced into the reactor with a reciprocating flow for cleavage of organic peroxides in the product and for dehydration DMFC.

Ways to prevent pollution in the rest of the pure phenol by hydroxyacetone (HA) described in BP 1 231 991, U.S. patent 5 064 507, etc. In accordance with BP 1 231 991 product of the oxidation of cumene, which mainly consists of CSB is subjected to the reaction of the acid cleavage and the reaction mixture is distilled to separate the raw (untreated) phenol from acetone, the low-boiling components (e.g., hydrocarbons and high-boiling components (e.g., unreacted DMFC, cumylphenol and methylstyrene dimer); crude phenol is treated with cation exchange resin so that to HA in the crude phenol turned in an easily detachable B4 507 crude phenol is treated with an organic polyamines, resulting HA in the crude phenol reacts with added organic polyamines with the formation of high-boiling compounds, which is then separated from the crude phenol in the distillation column.

However, these methods only complicate the method for production of phenol and require expensive equipment to remove HA. Thus, the regulation of education cumylphenol, methylstyrene dimer and other high-boiling components, which will reduce the yield of the final products, as well as education HECTARES, which will reduce the quality of pure phenol is critical for the commercial implementation of this method the cumene-phenol.

The publication of the last examination of the Japan patent N 51408/1990 describes the two-stage method. In the first stage used the back mixing reactor for the reaction when the concentration of sulfuric acid, 30 - 100 m D. (PPM) and temperature of 50 - 90oC, so that the concentration of HC in the reaction mixture is reduced to 0.5 - 5 wt.%. In the reaction of the first stage of the transformation DMFC in dicumylperoxide (marked as "DCT") is at least 40%. The reaction product of the first stage is then sent to the reactor with a piston flow, where the second reaction stage is carried out at 120 - 150oC for readiny way. In the first stage, the reaction is performed in a non-isothermal reactor at a concentration of acid catalyst 150 - 500 wt.m.D. and at a temperature of 50 - 62oC in the presence of added acetone, so that the concentration of the MSE is reduced to 0.3 to 1.5%. After mixing with the aqueous ammonia, the reaction product of the first stage is sent to the reactor piston flow and the second reaction stage is carried out at a temperature of 80 - 110oC for splitting DCT formed in the reaction of the first stage.

A critical issue in the reaction catalyzed by acid cleavage KGP is that the rate of this reaction is very rapid, the half-life is only a few seconds, and that the heat generated during the cleavage reaction, several times more than the heat, which is released in the usual exothermic reactions of organic chemistry. Therefore, if a few percent of CSB is cleaved immediately due to changes in the reaction conditions, the temperature of the reaction mixture will rise sharply and acetone, which is a low-boiling component of the reaction mixture will evaporate, increasing the pressure in the reactor and possibly causing an explosion of the reactor. Therefore, for the success of multi-stage method, in which neph and yet the final products are obtained with high yields.

A brief statement of the substance of the invention.

The purpose of this invention is to develop a method by which as phenol and a-MS, can be obtained stably with high yield under mild reaction conditions with adjustable formation of HA.

In order to achieve this goal, the applicants of this invention have conducted intensive studies on the above problems to select the multi-stage method (schema) in the way the cumene-phenol. As a result, they found that Cumyl-phenol and methylstyrene dimer, which will reduce the outputs of phenol and a-MS, more likely, are formed with increasing concentration of the a-MS in the reaction mixture. More specifically, the reaction mixture in the reactor back mixing is homogeneous, so that the composition of the reaction mixture in the reactor is identical to the composition of the mixture at the exit of the reactor. Therefore, carrying out the reaction for obtaining a-MS of DMPC inside the reactor back mixing leads to the formation of high concentrations of a-MS in the reactor. The applicants of this invention have found that it caused increased formation of cumylphenol and methylstyrene dimer, both of which were more severe (high) forms a MC. Applicants have found that regulation is newim flow, which will allow the reaction mixture to modify the composition of the development of the reaction, namely, the reactor type, which will provide a heterogeneous mixture. The best results were achieved by diluting the reaction mixture with a solvent. The preferred solvent is acetone, which is a major component of the reaction mixture has the lowest boiling point. It has been found that it is economical for the circulation of the solvent between the reactor in a subsequent stage distillation column.

As already mentioned in connection with the prior art, HA it is difficult to separate from phenol by distillation, and it will degrade the phenol, if it contaminates the rest of the pure final product. This HA is formed from acetone in the presence of PCG. Acetone is formed in a molar quantity equal to the molar quantity of the MSE, which cleaves the acid catalyst, and therefore it is difficult to guarantee that HA will not be formed at all. However, the applicants of this invention have found that the formation of HA can be reduced by conducting the acid cleavage MSE at low concentrations of acetone, namely, without the addition of acetone, separated in the distillation zone.

Based on these data and as-MS of the product cumene oxidation in the regulation of education HA which will degrade the quality of the rest of the pure phenol, it is preferable to divide the reaction into two or more stages and to carry out corresponding reactions in suitable conditions.

Accordingly, to achieve the above objective, the invention proposes a method for production of phenol, acetone and a-methylstyrene from the product of the oxidation of cumene containing cumonherface, cumene and dimethylphenylcarbinol, in the presence of sulfuric acid, characterized in that it includes a stage of decomposition cumonherface in the reactor back mixing with the release of a-methylstyrene, formed from dimethylphenylcarbinol regulated to not more than 35%, and the stage of formation of a-methylstyrene conducted in such a way that the reaction mixture formed in the first stage, served in a reactor with a piston flow when added to this reaction mixture of acetone.

Detailed description of the invention.

The method of this invention for the production of phenol (hereinafter referred to simply as "the method of the invention will now be described in detail.

The method of the invention is a method for production of phenol, acetone and a-MS of the product of the oxidation of cumene containing the MSE as the manner for carrying out catalyzed by acid cleavage of CSB in the back mixing reactor, and the reaction of the second stage, intended mainly to obtain a-MS in the reactor with reciprocating thread.

In the first stage of the method of the invention MSE, which is the main component source material (i.e. the product of the oxidation of cumene) liquor phenol and acetone in the back mixing reactor in the presence of sulfuric acid. The product of the oxidation of cumene, which serves as starting material, is obtained by first oxidizing cumene with air or oxygen at a temperature of about 100oC in the presence of sodium carbonate and then separating unreacted cumene from the oxidation product, in order to obtain a certain concentration of CSB in the distillation column. The product cumene oxidation typically has the following composition, wt.%:

KGP - 65 - 85

DMPC - 2 - 10

The cumene - 15 - 35

The acetophenone - 0,2 - 2

The reaction of the first stage, which is carried out in the method of this invention is the reaction for the production of phenol and acetone from PSC regulation education and-MS and GA. In this reaction the first stage, preferably the transformation of KGP in the range of 97 to 99.5%, preferably 98 - 99,0%, and the output of and-MS generated from dimethylphenylcarbinol, the product cumene oxidation desirable not higher than 35%, that is, memorial plaques and the reaction temperature of 55 - 80oC. In accordance with the description of the publication of the last examination of the Japan patent N 9971/1958, the temperature for carrying out reactions catalyzed by acid cleavage of CSB and education, and-MS is preferably in the range of 50 - 80oC. If the temperature of the reaction catalyzed by acid cleavage of CSB in this invention is higher than that specifically stated in the publication of the last examination of the Japan patent N 9971/1958 will occur thermal decomposition of the MSE, leading to lower yields of phenol and acetone. If the reaction temperature is excessively low, the removal of heat of reaction requires expensive equipment, and in addition, in the continuous reaction is observed instability temperature. In the method of the present invention use a lower concentration of sulfuric acid than in the method described in the publication of the last examination of the Japan patent N 9971/1958, the range of optimum temperature for the method of the invention is narrower than the range of temperatures specified in this patent publication.

In the method of this invention the concentration of water for carrying out reactions catalyzed by acid cleavage of CSB and education, and-MS of previ N 9971/1958, the concentration of water for the reaction should be controlled so as to ensure the formation of a homogeneous reaction mixture. Even if the reaction mixture is homogeneous, an excessively high concentration of water will reduce the strength of sulfuric acid used as the catalyst, thus increasing the concentration of HC in the reactor. Consequently, the use concentration of water is higher than the upper limit specified specifically for the practice of the method of the invention is not preferable.

Thus, compared with the single-stage scheme for carrying out reactions catalyzed by acid cleavage of CSB and education-MS, the reaction of the first stage of the method of the present invention is carried out in mild conditions, characterized by low concentration of sulfuric acid, as a result of this DMFC, which is as a by-product in the original product of the oxidation of cumene, or converted into DCT, which is a reaction product with KGP, or there is unreacted in the reaction mixture, resulting in regulation of transforming DMPK and in-MS.

During long-term operations of large systems in the industrial setting of the reaction conditions will vary Bo shall be at a minimum level. The operating stability of this method for production of phenol and acetone from KGP affected by changing the strength of the acid catalyst and the reaction temperature. Fortress acid catalyst susceptible not only to increase the water concentration in the reaction solution, but also to a concomitant sodium salt in the original product cumene oxidation, reduced the fortress acid will inhibit the decomposition of the MSE, thereby causing it to accumulate in the reactor. Therefore, to reduce the impact of changes to the terms of this method, and thereby to ensure that the concentration of HC in the reaction product is maintained constant, the reaction should be carried out with the concentration of acid catalyst, which is supported by not less than 100 wt. M. D. , preferably not less than 150 wt. M. D. the Concentration of acid catalyst in the range from 30 to 100 wt. memorial plaques is so small that it is difficult to ensure stable operation over a long period of time.

The residence time of the reaction mixture in the reactor back mixing is from 5 to 40 minutes and it is usually set in the range from about 15 to about 30 minutes

Heat of reaction which is released when a PSC split keys is in organic chemistry. Therefore, in the first stage reaction temperature in the reactor back mixing should be adjusted in such a way that the heat of reaction was completely removed in order to maintain a specific temperature of the reaction, resulting in the rate of cleavage of the CAS is maintained constant to ensure that the reaction mixture has a constant composition from the reactor exit back mixing before entering the second reactor stage. With this purpose it is necessary to get the reactor back mixing was a device suitable for regulating the temperature in the reactor so that it was permanent. To control the reaction temperature, so it was a constant, preferably using the method of irrigation acetone, in which the pressure in the reactor is reduced to the vapor pressure of the reaction mixture and latent heat of vaporization of the evaporated acetone is removed to maintain the temperature in the reactor at a constant level; alternatively, a portion of the reaction mixture in the reactor is removed and passed through a cooling heat exchanger so that the emitted heat of reaction to be removed before returning this part of the mixture in the reactor.

In the method of the present invention, the reaction mixture leaving the reaction is, The KP and the hydroperoxide as the main component. This reaction mixture was fed into the reactor with reciprocating flow for the reaction of the second stage, mainly to get a-MS of DMPC or DCT in the reaction mixture.

In the method of this invention the reaction of the second stage is carried out with acetone, which is added to control the reaction, which will be the formation of cumylphenol or methylstyrene dimer of a-MC. Add acetone preferably is the type of acetone, which is isolated by means of a separator, for example, distillation columns, from the reaction product leaving the reactor piston flow after the second stage, and which return in the same reactor with reciprocating thread.

The number of added acetone in the reaction of the second stage should be 1.15 - 1.8 times greater than the concentration of acetone in the reaction of the first stage.

The purpose of adding acetone in the reaction of the second stage is to reduce the concentration of a-MS in the reactor of the second stage, whereby the adjustment of the reaction, which leads to the formation of more severe forms of a-MS and which will reduce the yield of phenol and a-MS. As just mentioned above, the number of added acetone to the quality of acetone is effective for further regulation of the reaction, which leads to the formation of more severe forms of a-MS, but, on the other hand, more acetone is required for circulation between the reactor and the distillation column of acetone, which causes a corresponding increase in energy consumption for distillation of acetone, and this will lead to the adverse outcome from the point of view of the General economy. If adding acetone excessively small, it is unlikely to be effective to control the reaction, which leads to the formation of more severe forms of and-MS.

In the method of this invention it is unlikely that the formation of more severe forms of a-MS runs in the first reaction stage. This can be explained as follows: in the first stage reaction, the concentration of sulfuric acid used as the catalyst, is so small that DMFC will be the reaction of dehydration condensation with PCG education DCT and less likely that dehydration him in as-MS. As a result, the concentration of a-MS in the back mixing reactor small enough to guarantee that practically it is unlikely that the response of higher education forms and-MS. Therefore, if acetone is added to the first reaction stage, its effectiveness in regulirovaniya the second stage. In other words, the outputs of phenol and a-MS, which are formed when acetone is added in the first reaction stage, essentially comparable to the yields obtained by adding acetone to the reaction of the second stage. As already noted in connection with the review of prior art in this field, an excessively high concentration of acetone in the reaction of the acid cleavage MSE increases the formation of HA, which will degrade the quality of the rest of the pure phenol. The reaction of the first stage, carried out in the method of this invention, is intended mainly for the implementation of the acid cleavage KGP, adding acetone to the reaction of the first stage will be to increase the formation of HA, which leads to deterioration of quality in the rest of the pure phenol.

On the other hand, the reaction of the second stage is intended mainly for obtaining and-MS and acid cleavage KGP actually would not occur; therefore, will not improve education HA, even if acetone is added to the second reaction stage. Therefore, the outputs of phenol and a-MS, which receive, when acetone is added to the second reaction stage, comparable to the outputs achieved by adding acetone to the reaction of the first stage, and yet education is Teploobmennik thus, so it was heated up to 80 - 100oC before it is conducted in an adiabatic reactor with reciprocating thread.

If the reaction temperature of the second stage increases, it increases the reaction rate, leading to the necessity to shorten the reaction time. In the case where the reaction temperature of the second stage exceeds 120oC, the rate of formation which are byproducts of cumylphenol and methylstyrene dimer, which represent a more severe form of a-MS, will dramatically increase if the DCT transformation and DMPC in as-MS will be 70% or higher. Therefore, if the response of the education and MS carried out at a temperature higher than the upper limit of the reaction of the second stage in the method of the present invention, the interval, which allows for appropriate regulation of the reaction becomes so narrow that it can be quite difficult to regulate long-term operation in industrial plants.

The reaction of the second stage for the formation of a-MS of the DCT exothermic, so if it is conducted in an adiabatic reactor with a piston flow reactor non-isothermal condition is dominant, this leads to the fact that the temperature at the exit of the reactor is higher than the temperature at the entrance. More specifically,e is subjected to the second reaction stage, typically ranges from about 8 to about 20oC. Preferably, the temperature at the exit of the reactor of the second stage was no more than 120oC, preferably not more than 115oC, and it is necessary to increase the temperature of the reaction mixture in the first reaction stage was set so that the temperature of the reaction mixture at the exit of the reactor of the second stage does not exceed the above upper limit.

It is also necessary to ensure that the opposing reverse mixing the reaction mixture in the reactor of the second stage working piston flow, by increasing its length in comparison with the inner diameter or by creating in the reactor walls. The residence time of the reaction mixture in the reactor of the second stage working piston flow, usually from about 5 to about 30 minutes, preferably from about 8 to about 20 minutes

If the reaction of the second stage for the formation of a-MS of the DCT and DMFC ends in a reactor equipped with reciprocating flow of the method of the present invention, the reaction is quenched by immediately cooling the reaction mixture and neutralizing the sulfuric acid used as the acid catalyst. If an acid catalyst remains in reactio is to continue even after the cleavage reaction of organic peroxides and this will reduce the outputs of the and-MS and phenol. To circumvent this problem, an acid catalyst must be neutralized as soon as the end cleavage reaction of organic peroxides.

Sulfuric acid, which is acidic catalyst in the reaction mixture can be neutralized in accordance with the method, which is applied either caustic soda or sodium carbonate, or sodium phenolate, which is a salt of sodium hydroxide to phenol.

Neutralized reaction product is then subjected to distillation in such a way as to divide it into acetone, phenol, a-MS, cumene, etc. part of the separated acetone recycle for use as a diluent in the reaction of the second stage. Distillation of the neutralized reaction product is conducted to the distillation column at atmospheric or subatmospheric pressure.

Crude acetone obtained in the way the cumene-phenol to obtain the phenol contains aldehydes, alcohols, water, etc. Among these compounds aldehydes and water are compounds that are difficult to separate by distillation and consume a lot of energy for cleanup operations. Consequently, the use of purified acetone as a diluent for the reaction mixture is inefficient and increases the cost of production genocidally (raw) acetone, the aldehydes in the crude acetone can evolve into a more severe form under the act as a catalyst for sulfuric acid in the reaction mixture, so that its recycle at this concentration without accumulation in the distillation column.

The concentration of aldehydes in the crude acetone for use as a diluent for the reaction mixture in the second reaction stage is in the range from 100 to 5000 wt M. D., preferably from 500 to 2500 wt M. D. the Concentration of water in the crude acetone is in the range from 0.3 to 3 wt.%, preferably from 1 to 2 wt.%. If the concentration of aldehydes or water in the crude acetone is reduced, there is a noticeable increase in the consumption of energy required for the distillation operation. On the other hand, if the concentration of aldehydes or water in the crude acetone is increased, the reaction mixture was diluted in the reaction of the second stage will contain an increased amount of water and then the reaction efficiency will be reduced.

Specific examples of the present invention

The following examples and comparative examples are given to further illustrate this invention, but in no way should be taken as a limitation.

Example 1.

To the water and concentrated to obtain the product of the oxidation of cumene, which had the following composition, wt.%:

KGP - 81,0

DMPC - 5,2

The acetophenone - 0,8

The cumene is 13.0

The product of oxidation of cumene was served in a multistage reaction system comprising a reactor back mixing of the continuous type, with teplodessa ability, and adiabatic reactor with reciprocating thread. In a multistage reaction system was performed sequentially two reactions, the decomposition of the MSE in the first stage and the education and MS in the second stage.

The first stage reaction was carried out at a temperature of 60oC and the concentration of sulfuric acid 200 wt. memorial plaques for the time spent in this stage reactor 20 minutes the temperature of the first stage reactor was maintained constant by removing heat the reaction mixture under stirring. Continuously added 5% aqueous sulfuric acid solution, to ensure that the concentration of sulfuric acid in the reactor will be maintained 200 m D. as a result, the conversion of CAS to another component was 98.9 per cent and the output of and-MS obtained from DMPC was 18,0%.

Then acetone was added in a quantity which is 1.4 times higher than the concentration of acetone in the reaction mixture of the first stage. Added acetone was separated from naturalizovannye below, than acetone and 1.8 wt.% water. The reaction mixture of the first stage were then heated in a heat exchanger and sent to a reactor equipped with reciprocating flow for the reaction of the second stage. The residence time of the reaction mixture in the reactor of the second stage was 10 minutes ; the temperature at the exit of the second stage reactor was 110oC; the reaction mixture of the second stage had a water concentration of 1.0 wt.%. The final reaction product was analyzed to determine the yields of phenol and a-MS, as well as the concentration of HA. The results are given in table. 1.

Example 2.

The product of oxidation of cumene obtained as in example 1 was subjected to reaction in the reaction system of the same type as described in example 1. The first stage reaction was carried out at 60oC and the concentration of sulfuric acid 250 wt. memorial plaques for the residence time in the reactor 15 minutes Continuously applied 5% aqueous solution of sulfuric acid, to ensure that the concentration of sulfuric acid in the reactor will be maintained 250 wt. M. D. Conversion of CAS to other components in the reaction of the first stage was 98.7 per cent and the output of and-MS obtained from DMPC was 16.2 per cent.

Then acetone was added in a quantity which is 1.54 times higher than the concentration of acetone in the reaction mixture of the first stage. the stings 1000 wt. M. D. aldehyde having a boiling point lower than that of acetone and 1.8 wt.% water. The reaction mixture of the first stage were then heated in a heat exchanger and sent to a reactor equipped with reciprocating flow for the reaction of the second stage. The residence time of the reaction mixture in the reactor of the second stage was 21 min; the temperature at the exit of the reactor of the second stage was 113oC; the reaction mixture of the second stage had a water concentration of 1.4 wt.%. The reaction product of the second stage were analyzed to determine the yields of phenol and a-MS, as well as the concentration of HA. The results are given in table. 2.

Example 3.

The product of oxidation of cumene obtained as in example 1 was subjected to reaction in the reaction system of the same type as described in example 1. The first stage reaction was carried out at a temperature of 75oC and the concentration of sulfuric acid 120 wt. memorial plaques for the residence time in the reactor 15 minutes Continuously applied a 2.5% aqueous solution of sulfuric acid, to ensure that the concentration of sulfuric acid in the reactor will be maintained 150 wt. M. D. Conversion of CAS to other components in the reaction of the first stage was to 99.1% and the output of and-MS obtained from DMPC was 21.0 per cent.

Then acetone was added in a quantity which is 1.54 times higher than the th reaction product of the second stage by distillation, it contained 1000 wt. M. D. aldehyde having a boiling point lower than that of acetone and 1.8 wt.% water. The reaction mixture of the first stage were then heated in a heat exchanger and sent to a reactor equipped with reciprocating flow for the reaction of the second stage. The residence time of the reaction mixture in the reactor of the second stage was 17 minutes ; the temperature at the exit of the reactor of the second stage was 108oC; the reaction mixture of the second stage had a water concentration of 1.4 wt.%. The reaction product of the second stage were analyzed to determine the yields of phenol and a-MS, as well as the concentration of HA. The results are given in table. 3.

Comparative example 1.

The product of oxidation of cumene obtained as in example 1 was subjected to reaction in the reaction system of the same type as described in example 1. Acetone was added to the reaction mixture of the first stage, but acetone was added in the second reaction stage. The first stage reaction was carried out at 75oC for a residence time in the reactor 15 minutes Continuously applied to the solution containing 2000 wt. M. D. sulphite acetone, to ensure that the concentration of sulfuric acid in the reactor will be maintained 260 wt. memorial plaques were Added acetone was separated from the neutralized reaction product of the second stage of discrace acetone reaction mixture was 1.3 times more of this magnitude in the case where acetone was added. The transformation of KGP in another component in the reaction of the first stage was 98.5% and the output of and-MS obtained from DMPC was 29.0 percent.

Then the reaction mixture of the first stage was heated in a heat exchanger and fed into the reactor with a reciprocating flow for the reaction of the second stage. The residence time of the reaction mixture in the reactor of the second stage was 17 min, the temperature at the exit of the reactor of the second stage was 108oC and the reaction mixture of the second stage had a water concentration of 1.4 wt.%. The reaction product of the second stage were analyzed to determine the yields of phenol and a-MS, as well as the concentration of HA. The results are given in table. 4.

Comparative example 2.

The product of oxidation of cumene obtained as in example 1 was subjected to reaction in the reaction system of the same type as described in example 1. The first stage reaction was carried out at 70oC and concentration of sulphuric acid 500 wt. memorial plaques for the residence time in the reactor 20 minutes Continuously applied 5% aqueous solution of sulfuric acid, to ensure that the concentration of sulfuric acid in the reactor will be maintained 500 wt.m.D. The transformation of KGP in another component in the reaction of the first stage was 99.7%, and the output of and-MS obtained from DMPC was 39.4 percent.

oC; the reaction mixture of the second stage had a water concentration of 1.7 wt.%. The reaction product of the second stage were analyzed to determine the yields of phenol and a-MS, as well as the concentration of HA. The results are given in table. 5.

Thus, in accordance with the method of this invention, the phenol and a-MS can be obtained in high yields with less education HECTARES and in addition, the process of this production is very stable. Therefore, the method of the present invention is of great value for practical application.

1. Method for production of phenol, acetone and a-methylstyrene from the product of the oxidation of cumene containing cumene hydroperoxide, cumene and dimethylphenylcarbinol, including the cleavage of cumene hydroperoxide in the Pris is at 55 - 80oC, and using the second stage reactor piston type with a temperature higher than in the reactor in the first stage, characterized in that the reactor reverse mixing process leading to conversion of dimethylamine not less than 35%, add acetone to the reaction mixture and then it is directed into the reactor piston type.

2. The method according to p. 1, characterized in that the cleavage of cumene hydroperoxide obtained by the oxidation of cumene lead in the reactor back-mixing in the presence of 150 - 350 wt. M. D. sulfuric acid.

3. The method according to p. 1, characterized in that at the stage of education-methylstyrene in the reactor with a piston flow in the reaction mixture was added acetone in an amount such that the concentration of acetone was 1.15 - 1.8 times more than in the zone of the reactor back-mixing.

4. The method according to p. 1, characterized in that the water concentration in the reaction mixture is maintained within the range of 0.5 to 3.0 wt.%.

5. The method according to p. 1, characterized in that the product of the oxidation of cumene containing cumene hydroperoxide, dimethylphenylcarbinol, acetophenone and cumene, served in the reactor back-mixing, in which the cumene hydroperoxide break down in the presence of 150 - 350 wt. M. D. sulfuric collocalia removing the heat of reaction for the cleavage of cumene hydroperoxide by reducing the pressure in the reactor of the inverse mixing until the vapour pressure of the reaction mixture, remove the latent heat of vaporization of the evaporated acetone, and recycling the liquid acetone in a reactor of reverse confusion.

6. The method according to p. 1, characterized in that the product of the oxidation of cumene containing cumene hydroperoxide, dimethylphenylcarbinol, acetophenone and cumene, served in the reactor back-mixing, in which the cumene hydroperoxide break down in the presence of 150 - 350 wt. M. D. sulfuric acid to form phenol and acetone, at a temperature in the reactor of the inverse mixing 55 - 80oC, which is established by removing the heat of reaction for the cleavage of cumene hydroperoxide by removal of the reaction mixture by passing it through a heat exchanger to remove heat of reaction for the cleavage of cumene hydroperoxide, and recirculation of the mixture in the reactor back-mixing.

7. The method according to p. 5 or 6, characterized in that raceplane cumene hydroperoxide carried out until the degree of conversion of cumene hydroperoxide 97,0 - 99,5%.

8. The method according to p. 5 or 6, characterized in that the cleavage of cumene hydroperoxide carried out until the degree of conversion of cumene hydroperoxide 98 - 99%.

9. Method for production of phenol from cumene oxidation and subsequent decomposition of the received hydroperoxyalkyl and dicumylperoxide, in which phenol and acetone are present in equimolar amounts, characterized in that the reaction mixture was added acetone in an amount of 1.15 to 1.8 times its original concentration, after which the mixture is fed into the reactor with reciprocating flow for dehydration dimethylphenylcarbinol and splitting dicumylperoxide.

10. The method according to p. 9, characterized in that after the addition of acetone, the reaction mixture is heated to 80 - 100oC in the heat exchanger.

11. The method according to p. 10, wherein the heated reaction mixture is served in the non-isothermal reactor with piston flow to obtain-methylstyrene from dimethylphenylcarbinol and dicumylperoxide.

12. The method according to p. 9, characterized in that at the outlet of the reactor piston flow keep the temperature of the reaction mixture not exceeding 120oC.

13. The method according to p. 9, characterized in that at the outlet of the reactor piston flow keep the temperature of the reaction mixture not exceeding 115oC.

14. The method according to p. 9, characterized in that the reaction mixture leaving the reactor piston flow, immediately cooled and neutralized to stop the reaction.

15. The method according to p. 14, characterized in that the m part of the separated acetone is added to the reaction product in the reactor back-mixing in such numbers, to the concentration of acetone in the reaction product was 35 - 50 wt.% before the specified reaction product is fed into the reactor with reciprocating thread.

16. The method according to p. 15, characterized in that the reaction product in the reactor back-mixing of acetone is added which contains the 100 - 5000 wt. M. D. aldehyde and 0.3 to 3.0% water.

 

Same patents:

The invention relates to the production of phenol and acetone "Kukolnik method, in particular to the improvement of the process of decomposition gidroperekisi hydroperoxide (CHP) acid catalyst to phenol and acetone

methylstyrene" target="_blank">

The invention relates to the field of petrochemical synthesis, in particular to a method for production of phenol, acetone and alpha-methylstyrene Kukolnik method

The invention relates to the creation of new highly active catalyst for the conversion of ethanol in acetone

The invention relates to the field of organic chemistry and petrochemicals, and in particular to catalysts for the production of phenol and acetone

The invention relates to the production of phenol and acetone "Kukolnik method, in particular to the improvement of the process of decomposition gidroperekisi hydroperoxide (CHP) acid catalyst to phenol and acetone

The invention relates to a method of obtaining a mixture containing cyclic saturated alkane and the corresponding alkanol

The invention relates to the production of phenol and acetone "Kukolnik method, in particular to the improvement of the process of decomposition gidroperekisi hydroperoxide (CHP) acid catalyst to phenol and acetone

The invention relates to a method of purification of phenol obtained in the process of co-production of acetone and phenol Kukolnik method

The invention relates to methods of cleaning product of phenol, the resulting acid-catalytic decomposition of cumene gidroperekisi

The invention relates to 4-methoxyethyl-2-tert.-butylphenol (1) (alkyl = ethyl-, propyl-), which is obtained by processing 4-chloroalkyl-2,6-di-tert.-butylphenols the sodium methylate or sodium hydroxide solution in methanol) under heating, followed by thermolysis of the resulting 4-methoxyethyl-2,6-di-tert
The invention relates to petrochemistry and can be used in the production of phenol and acetone Kukolnik method

The invention relates to the field of organic chemistry and petrochemicals, and in particular to catalysts for the production of phenol and acetone

The invention relates to catalytic methods reductive dechlorination of highly dangerous organic substances and can be used for detoxification of chlorinated aromatic compounds, in order to obtain the target products

The invention relates to the production of phenol and acetone "Kukolnik method, in particular to the improvement of the process of decomposition gidroperekisi hydroperoxide (CHP) acid catalyst to phenol and acetone

methylstyrene" target="_blank">

The invention relates to the field of petrochemical synthesis, in particular to a method for production of phenol, acetone and alpha-methylstyrene Kukolnik method
The invention relates to petrochemistry and can be used in the production of phenol and acetone Kukolnik method
Up!