Method of alkylen oxide production

FIELD: chemistry.

SUBSTANCE: invention refers to method of alkylen oxide production as involving (i) mixing the original raw stock containing organic hydroperoxide and alken with and recycled flow to prepare the reaction mixture containing alcohol 5 to 80 wt % per total amount of the reaction mixture; (ii) contacting the reaction mix and the heterogeneous epoxidation catalyst to make the flow containing alkylen oxide and alcohol; and (iii) recycling the flow 30 to 95 wt % from the stage (ii) to the stage (i).

EFFECT: method improvement.

9 cl, 1 ex

 

The present invention relates to a method for alkylen-oxide.

In the prior art it is known epoxidation of alkene in alkylene oxide in the reaction of the alkene with an organic hydroperoxide.

The above epoxidation reaction is used, for example, in a well-known method for simultaneous receipt of propylene oxide and styrene from ethylbenzene. Usually this method to simultaneously obtain two products involves the following stages (i) interaction of ethylbenzene with oxygen or air to form ethylbenzene hydroperoxide, (ii) interaction thus obtained cumene ethyl benzene with propene in the presence of an epoxidation catalyst with the formation of propylene oxide and 1-phenylethanol and (iii) the conversion of 1-phenylethanol in styrene as a result of dehydration using the appropriate catalyst for dehydration.

Another way to get alkylene-oxide is the simultaneous production of propylene oxide and methyl tert-butyl ether (MTBE from isobutene and propene. This method is well known in the prior art and includes a similar stage of the interaction, as in the method of producing styrene and propylene oxide described in the previous paragraph. Under epoxidation tert-butylhydroperoxide interacts with propene with the formation of propylene oxide and tert-butanol, prisutstvie heterogeneous epoxidation catalyst. Further, as a result of esterification of tert-butanol methanol receive MTBE, which is used as an additive for motor fuels.

An additional method includes obtaining propylene oxide using cumene. In this way the hydroperoxide reacts with oxygen or air with the formation of cumene hydroperoxide. The resulting cumene hydroperoxide interacts with propene in the presence of an epoxidation catalyst with the formation of propylene-oxide and 2-phenylpropanol. The latter can be converted into cumene using hydrogen and a heterogeneous catalyst. A corresponding method is described, for example, in patent application WO 02/48126.

The present invention relates to the epoxidation reaction between an alkene and an organic hydroperoxide using a heterogeneous catalyst.

In the technique known heterogeneous catalysts for epoxidation. Such catalysts may contain as catalytically active metal one or more transition metals, such as vanadium, molybdenum, tungsten, titanium and zirconium. One particularly suitable class of heterogeneous epoxidation catalysts are catalysts based on titanium. Examples of such catalysts are described, for example, in the application US-A-4367342 and EP-A-0345856. Application US-A-4367342 discloses the use of inorganic compounds of oxygen with silicon is m in the chemical composition, at least 0.1% wt. the oxide or hydroxide of titanium, while the application EP-A-0345856 reveals as a heterogeneous catalyst titanium dioxide on the silicon dioxide obtained by impregnation of a silicon compound in a stream of titanium tetrachloride with subsequent stages of annealing and hydrolysis and optional stage of sililirovanie.

When using such heterogeneous epoxidation catalysts to accelerate the reaction of alkene epoxidation catalyst slowly deactivates. It would be advantageous if the catalyst maintained a high activity over a long period of time, as this would reduce the cost of the catalyst and the time and costs associated with the restart of the reactors. In addition, the desired slower deactivation, as in this case it would be possible to maintain a lower average temperature. It was found that the lower the average temperature of the reaction leads to the formation of fewer by-products. Therefore, a higher activity of the catalyst allows a process with lower cost and higher performance.

In the patent application WO 98/32530 describes how to obtain epoxy compounds by reacting propylene with an organic hydroperoxide using a solid contact catalyst, in which the Colo 25-75% of the heat of reaction is removed by heating introduced into the reactor cold raw material in direct contact with the stream of heated propene from the reactor. In this way, is shown in figure 3, the partially reacted reaction mixture is divided into two parts, with one recyclery and mixed with cold raw material input, and the other sent to the next layer of catalyst. However, in the application there is no information on the number recyclorama the reaction mixture, or the degree of conversion. In addition, recyclable reaction mixture does not contain propylene, as described, that propylene is evaporated and removed prior to recycling of the reaction mixture.

In the patent application WO 01/1267 noted that the activity Deaktivierung catalyst can be restored by contact Deaktivierung catalyst with the reaction mixture of the process of epoxidation at a temperature that is at least 5C higher than the final temperature at which at least partially deactivated catalyst was used immediately prior to reactivation. In example 1, the deactivated catalyst is contacted with the raw material while maintaining the great value of recycling through the reactor in order to ensure the contact to be reactivated catalyst from the reaction product of epoxidation. When performance 48 grams/hour of raw materials and the recycling rate of 2.5 kg/h it turns out that recycled more than 98% wt. product. In the patent application WO 01/12617 used the t a large amount of recycling only to create conditions close to ideal mixing. But in the application WO 01/12617 no recommendations, no hint of the use of recycling to obtain alkylene-oxide.

In the application WO 01/12617 describes a typical raw materials for the process of epoxidation, containing 15-25% by weight. cumene ethylbenzene, 30-50 wt.%. ethylbenzene, 30-50 wt.%. of propene, 0-5 wt.%. 1-phenylethanol and 0-5 wt.%. methylvinylketone, total to 100 wt.%.

The inventors have developed a method that allows you to maintain high catalyst activity over a long period of time. Unexpectedly, it was found that deactivation of the catalyst is slower if you use recycling.

Therefore, the present invention relates to a method for alkylen-oxide, which includes

(i) mixing of fresh raw materials containing organic hydroperoxide and alkene, with recyclorama stream to obtain a reaction mixture containing from 5 to 80 wt.%. alcohol calculated on the total quantity of reaction mixture,

(ii) contacting the reaction mixture with a heterogeneous epoxidation catalyst to obtain a stream containing alkylene oxide and alcohol, and

(iii) recycling from 30 to 95 wt.%. obtained in stage (ii) of the flow to the step (i).

Not based on any theory, it is believed that the resulting application of recycling mainly who define the company associated with an increased alcohol content in the reaction mixture, contacted with the catalyst.

The reaction mixture, which is in contact with the catalyst for epoxidation, consists of fresh raw materials and recyclorama the reaction mixture. Usually fresh raw material will contain less than 5% wt. alkylene-oxide calculated on the total amount of the reaction mixture, more specifically, less than 3% wt. alkylene-oxide. Preferably, the fresh feedstock contains less than 1% wt. alkylene-oxide. More preferably, the fresh raw materials did not contain alkylene oxide.

Used in the present invention, the alkene can be any organic compound, at least one double bond between aliphatic carbon atoms. This connection will typically contain from 2 to 25 carbon atoms and preferably from 3 to 12 carbon atoms, e.g. propene, 1-butene, 2-butene, 1-penten, 1-octene, 1-dodecene, styrene and methylsterol. However, it is most preferable to use as the alkene propene, receiving, thereby propylene oxide in accordance with the method of the present invention.

Used organic hydroperoxide may be any suitable organic hydroperoxide. Organic hydroperoxides, which are widely used in industry, are tert-butyl hydroperoxide and the hydroperoxide of alkylaryl. The hydroperoxides of alkylaryl especially a preference for the equipment.

Specific hydroperoxides of alkylaryl are cumene hydroperoxide and ethylbenzene hydroperoxide. Used heterogeneous epoxidation catalyst may be any known in the prior art a catalyst for accelerating the reaction between the alkene and an organic hydroperoxide with the formation of the corresponding alkylene-oxide and alcohol. However, such catalysts are preferred. Accordingly, as discussed above, the catalysts disclosed in the descriptions of the patents US-A-4367342 and EP-A-0345856 may, for example, be used. However, it was found that the most advantageous to use all the epoxidation reactor for the purpose of the present invention the catalysts in the form of titanium dioxide on the silicon dioxide disclosed in EP-A-0345856. When using these catalysts, the present method gives very good results.

An industrial application of stage (ii) of the epoxidation reaction is usually carried out at temperatures from 50 to 135C, preferably from 70 to 125C. the Pressure can reach up to 80 bar, preferably from 10 to 60 bar. The preferred reaction medium is a liquid phase.

The composition used in the present invention the reaction mixture is not critical as long as there is a required amount of alcohol. Accordingly, in the case of the method of simultaneous floor is placed styrene and propylene oxide, the reaction mixture will typically contain some amount of cumene ethylbenzene, and usually a significant amount of ethylbenzene. In the case of a method of producing propylene oxide by using cumene hydroperoxide may contain a large number of cumene. If propylene oxide get together with methyl tert-butyl ether (MTBE), the reaction mixture may contain tert-butane.

Propene is added to the reactor or in separate input stream, or can add in fresh raw materials or recyclorama the reaction mixture prior to its entry into the reactor(s) epoxidation.

Fresh raw material can also contain a number of methylvinylketone and/or 1-phenylethanol formed in the preceding sections oxidation or during the previous epoxidation reactor or contained in recyclorama thread. Typical fresh feedstock contains 15-25% by weight. cumene ethylbenzene, 30-50 wt.%. ethylbenzene, 30-50 wt.%. of propene, 0-5 wt.%. 1-phenylethanol and 0-5 wt.%. methylvinylketone, total to 100 wt.%. This flow of fresh raw material combined with recyclorama flow in order to obtain the desired reaction mixture for use in the present invention.

The reaction mixture for use in stage (ii) of the present invention will typically contain at least 7% by weight. alcohol, more specifically, at least 8 wt.%. alcohol, preferably at least 10 wt.%. alcohol per summary the number of the reaction mixture. You can create a very high concentration of alcohol in the result of the addition of alcohol to those already present in recyclorama the flow of alcohol. As such alcohol can, in principle, be any alcohol. However, this alcohol is preferably an alcohol formed from used in the present invention organic hydroperoxide, and it can be obtained from another part of the plant in pure or less pure form.

A very high content of alcohol has the disadvantage that as the concentration of reagents in the reaction mixture decreases. Therefore, it is generally preferable that the alcohol was present in amount of less than 80% wt., more preferably not more than 60 wt.%, more preferably not more than 50 wt.%, more preferably not more than 40 wt.%, and most preferably not more than 30% wt. Typically, the reaction mixture in stage (ii) will contain from 10 to 40% wt. the alcohol.

Alcohol, which is mainly according to the present invention is present in the process is the product of the conversion of organic hydroperoxide. If applied tert-butyl hydroperoxide, alcohol is tert-butanol. If using ethylbenzene hydroperoxide, alcohol is 1-phenylethanol. If used cumene hydroperoxide, alcohol is 2-phenylpropanol.

More specifically, the reaction mixture on the adiya's (ii) contains from 3 to 25 wt.%. organic hydroperoxide, from 20 to 50% wt. alkene, from 5 to 50% wt. alcohol and from 0 to 60 wt.%. additional compounds in the amount up to 100% wt. More preferably, the reaction mixture in stage (ii) contain from 5 to 20% wt. organic hydroperoxide, from 30 to 50% wt. alkene, from 5 to 40% wt. alcohol and from 0 to 60 wt.%. additional compounds, in an amount up to 100% wt. More specifically, the reaction mixture in stage (ii) contains from 5 to 20% wt. organic hydroperoxide, from 30 to 50% wt. alkene, from 5 to 25% wt. alcohol and from 5 to 60 wt.%. additional compounds, in an amount up to 100% wt.

Preferably, the reaction mixture, which recyclery with stage (ii) at stage (i), underwent conversion to a certain extent, in order to have the required amount present in the mixture of alcohol. Therefore, it is preferable that recyclery flow of product contained not more than 15% wt. organic hydroperoxide, more specifically, not more than 10% wt. organic hydroperoxide. Most preferably, recyclable reaction mixture contains from 0.5 to 10% wt. organic hydroperoxide. In addition, recyclable reaction mixture usually contains a significant amount of the alkene, as alkene is usually present in molar excess, and only part of the hydroperoxide is usually converted. Usually recyclable reacts the traditional mixture contains from 10 to 50% wt. alkene. This is a difference from being recycled stream, which is used in the patent application WO 98/32530.

Recyclery stream may be combined with fresh raw material in a wide range of ratios. Preferably, the mass ratio being recycled stream stage (iii) to fresh raw materials ranged from 0.5 to 4, more specifically, from 1 to 3, most specifically, about 2.

When using recycling can be difficult to achieve practically complete conversion of the organic hydroperoxide, as it requires a relatively long time. The embodiment of the present invention is that a large part of the organic hydroperoxide is converted in the presence of the stream being recycled, while the final conversion is carried out in the absence of being recycled stream. Therefore, the present invention preferably further includes (iv) contacting the remainder of the stream obtained in stage (ii), with an additional catalyst for the epoxidation of obtaining the product stream, containing no organic hydroperoxide. It was found that at this stage of the process does not require the presence of added alcohol to maintain high catalyst activity for a long time.

In a particularly preferred variant of the invention, stage (iv) Provo is Yat, at least 2 separate reactors, in order to be able if necessary to replace the catalyst without stopping the process. It was found that the most beneficial if these reactors arranged in series.

In a preferred embodiment of the present invention, the reaction mixture is contacted on a stage (ii) catalyst for the epoxidation of at least 2 parallel reactors, and more particularly, from 2 to 5 parallel reactors. The use of parallel reactors allows the reaction mixture to contact with a catalyst of different activity. The amount of materials sent to each parallel reactor may vary depending on the activity of the catalyst present in the reactor. This mode leads to optimum use of the present catalyst. In addition, the use of parallel reactors allows you to replace the catalyst without stopping the process.

Depending on the situations that arise can be advantageous to make contact with fresh catalyst with the raw materials with different molar ratio of alkene to the hydroperoxide than with catalyst, the former in operation for some time. Preferred embodiments of such a mode is described in the still unpublished is Oh provisional patent application WO-A-03/082843.

Preferably, from 50 to 90 wt.%. flow obtained at stage (ii), recycled as the reaction mixture, more particularly, from 60 to 80 wt.%.

The method of integration of heat in the present invention depends to a very large extent on the particular circumstances. The use of recycling leads to heating of fresh raw materials blending with recyclorama stream stage (ii), which typically has a higher temperature. Temperature being recycled stream can be lowered by engagement of the end product, containing no organic hydroperoxide, such as, for example, obtained at an optional stage of the process (iv), in the heat exchanger recyclorama part of the stream obtained in stage (ii).

The alcohol obtained in stage (ii) and/or stage (iv), can be transformed further by any well-known specialist in this field of technology by the way. If the organic hydroperoxide was cumene hydroperoxide, we obtain 2-phenylpropane-2-ol can be gidrirovanny back to cumene. If the organic hydroperoxide was the ethylbenzene hydroperoxide, it is preferable that the method further include the separation of 1-phenylethanol from the product stream and the dehydration of 1-phenylethanol by using a dehydration catalyst to obtain styrene. If the organic hydroperoxide was Gidropark the ID tert-butyl, it is preferable that the method further include the interaction of methanol with tert-butanol to obtain MTBE.

The invention is further illustrated by the following examples without limiting the scope of the invention to these specific choices of implementation.

Example

The examples were carried out on a continuous flow laboratory setup for epoxidation with two tanks on automatic balancer balancing, containing, respectively, the flows of ethylbenzene hydroperoxide and enter the alkene, two pumps of a high pressure reactor with a fixed layer, a third pump for transmission stream being recycled through the reactor, means for maintaining in the reactor a constant desired temperature between 50 and 140C, a Stripping column for removal of boiling components, such as alkene, a refrigerator and a reservoir for reception of the product.

Source reagents were applied to the reactor by means of two high-pressure pumps and mixed together before introduction into the reactor. The reactor was operating in the liquid phase at a pressure of 50 bar. The temperature of the injected raw material in the reactor was about 90C. If required, the product can be recycled and combined with fresh raw material with the help of the third pump. The remaining product was otparyvali, cooled and stored. If you have used the recycling stream, the source is propene and the ethylbenzene hydroperoxide in solution of ethyl benzene was mixed with recyclorama stream prior to introduction into the reactor.

The catalyst for the epoxidation was containing titanium on silica catalyst, which was prepared as described in example according to the method of application EP-A-345856. Were loaded into the reactor a total of 21 grams of catalyst.

Used organic hydroperoxide contained from 30 to 40% wt. of ethylbenzene hydroperoxide in ethylbenzene. Fresh raw material was obtained by mixing of propene and solution of ethylbenzene hydroperoxide in such quantities that the molar ratio of propene to ethylbenzene hydroperoxide was about 6.

The flow rate of raw material is continuously changed so that the conversion of ethylbenzene hydroperoxide was approximately constant around 80%.

The reaction rate constant epoxidation of the second order (k0) was determined on the assumption that the reaction rate by hydroperoxide, ethyl benzene and propene are the first order.

Comparative example 1

In comparative example 1 recycling the received output stream is not used. Within 20 days of work was achieved conversion of 80% when using a flow rate of 333 g/hour. Concentration of cumene ethyl benzene and propene during this time to calculate the k0and took the value 1.

Example 1

In example 1 recycled 2/3 of the product. Within 20 days of 420 g/h was introduced into the reactor and mixed with 840 g/h being recycled leaving is his thread. The combination of fresh raw materials being recycled and the exit stream contained about 13% by weight. 1-phenylpropanol. The total conversion of fresh raw materials through the reactor amounted to 78.9 per cent. The concentrations of cumene ethyl benzene and propene during this time to calculate the k0and it was found that it is 1.6 times more than the k0calculated in the comparative example.

1. The method of obtaining alkylene-oxide, including
i) mixing of fresh raw materials containing organic hydroperoxide and alkene, with recyclorama stream to obtain a reaction mixture containing from 5 to 80 wt.% alcohol calculated on the total quantity of reaction mixture,
(ii) contacting the reaction mixture with a heterogeneous epoxidation catalyst to obtain a stream containing alkylene oxide and alcohol, and
(iii) recycling from 30 to 95 wt.% flow obtained at stage (ii), on stage (i).

2. The method according to claim 1, additionally including
(iv) contacting the remainder of the stream obtained in stage (ii), with an additional catalyst for epoxidation to obtain the product stream, containing no organic hydroperoxide.

3. The method according to claim 1 or 2, in which the reaction mixture is supplied to the step (ii)contains from 3 to 25 wt.% organic hydroperoxide, from 20 to 50 wt.% alkene, from 5 to 50 wt.% alcohol and from 0 to 60 wt.% additional compounds, the amount is but up to 100 wt.%.

4. The method according to claim 1 or 2, in which recyclery the product stream contains not more than 10 wt.% organic hydroperoxide.

5. The method according to claim 1 or 2, in which the reaction mixture is supplied to the step (ii)contains from 10 to 40 wt.% the alcohol.

6. The method according to claim 1 or 2, which comprises contacting the reaction mixture with a catalyst for the epoxidation of at least 2 parallel reactors at the stage (ii).

7. The method according to claim 1 or 2, in which the mass ratio being recycled stream obtained in stage (ii), to the fresh feedstock is from 0.5 to 4.

8. The method according to claim 1 or 2, in which the alkene is propene.

9. The method according to claim 1 or 2, in which the organic hydroperoxide is ethylbenzene hydroperoxide, and which further includes a separation of l-phenylethanol from the product stream and the dehydration of l-phenylethanol by using a dehydration catalyst to obtain styrene.



 

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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

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention proposes a method for synthesis of oxirane compounds comprising the following steps: (i) oxidation of alkylaryl to yield alkylaryl hydroperoxide; (ii) contacting at least lesser part of alkylaryl hydroperoxide prepared at the step (i) with olefin in the presence of catalyst to yield oxirane compound and alkylaryl hydroxyl; (iii) separation of oxirane compound from the reaction product from the step (ii), and (iv) contacting at least part of the reaction product no containing oxirane compound with hydrogen to yield alkylaryl and at least of part of the latter is re-circulated to the step (i) and wherein alkylaryl means an alkylaryl compound representing di-(isopropyl)-benzene. Invention provides the possibility for preparing oxirane compound without the necessity for preparing other compounds and reducing the amount of the parent alkylaryl.

EFFECT: improved method of synthesis.

3 cl

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention proposes a method for synthesis of oxirane compounds comprising 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 at the temperature range 0-200°C and under pressure in the range 1-100 x 105 H/m2 in the presence of a catalyst comprising titanium on silicon dioxide and/or silicate to yield oxirane compound and alkylaryl hydroxyl; (iii) optional interaction of at least part of alkylaryl hydroperoxide prepared at the step (i) to yield phenol and ketone; (iv) separation of oxirane compound from the reaction product from the step (ii0, and (v) contacting at least part of the reaction product no containing oxirane with hydrogen at temperature 100-330°C and under pressure 0.1-50 x 105 H/m2 in the presence of the hydrogenation catalyst to yield alkylaryl and at least part of the latter is re-circulated to the step (i) wherein the hydrogenation catalyst represents catalyst comprising copper compound, zinc compound and at least one compound chosen from the group consisting of aluminum, zirconium, magnesium rare-earth metals and their mixtures. Invention provides the possibility for synthesis of oxirane compounds without necessity for simultaneous synthesis of other compounds.

EFFECT: improved method of synthesis.

5 cl, 7 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for interaction of an organic compound with hydroperoxide. Invention describes a continuous method of interaction of organic compound comprising at least one C-C-double bond with hydroperoxide in the presence of a catalyst. Method involves interaction of organic compound at the reaction step (R1) under the range of the own pressure below 100 bars, temperature in the range 0-120°C and in the molar ratio of reacting organic compound to hydroperoxide in the range 0.7-20 with hydroperoxide in the presence of a zeolite-containing catalyst to yield at least one flow of the product (P1). Then at least one flow of the product (P1) is fed to intermediate treatment (Z1) wherein (Z1) forms at least one the hydroperoxide-containing product flow (PZ1) and wherein the intermediate treatment represents distillation separation of hydroperoxide from at least one the product flow (P1) or addition of a base to at least one the product flow (P1) and at least one the product flow is fed to at least in the reaction step (R2) wherein under pressure in the own pressure up to 100 bars, temperature in the range 0-120°C and in the molar ratio of the reacting organic compound to hydroperoxide in the range 0.7-20 hydroperoxide is subjected for interaction with an organic compound in the presence of a zeolite-containing catalyst to yield at least one the product flow (P2) wherein at least one of reaction steps (R1) and (R2) the method involves using the reactors system comprising at least two reactors joined in parallel. Also, invention describes a device for carrying out the interaction of an organic compound with hydroperoxide.

EFFECT: improved method for interaction.

9 cl

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to production of alkylaryl hydroperoxides useful as starting material in production of propylene oxide and alkenylaryl. Process of invention comprises following stages: oxidation of alkylaryl compound to form reaction product containing alkylaryl hydroperoxide; contacting at least part of reaction product with basic aqueous solution; separation of hydrocarbon phase containing alkylaryl hydroperoxide from aqueous phase; containing at least part of above hydrocarbon phase with aqueous solution containing waste water, said aqueous solution containing less than 0.2% alkali metal and/or salt (determined as ratio of metal component to total amount of solution); and separation of hydrocarbon phase from aqueous phase. By bringing at least part of above hydrocarbon phase containing alkylaryl hydroperoxide into interaction with propylene and catalyst, alkylaryl hydroxide and propylene oxide are obtained. At least part of propylene oxide is then separated from alkylaryl hydroxide. Dehydration of at least part of alkylaryl hydroxide results in formation of alkenylaryl.

EFFECT: reduced amount of contaminating by-products in alkylaryl hydroperoxide preparation stage.

8 cl, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to method for synthesis of alkylaryl peroxide-containing compound. Method involves the following steps: (a) oxidation of alkylaryl compound to yield the alkylaryl hydroperoxide-containing reaction substance; (b) treatment of at least part of the reaction substance containing alkylaryl hydroperoxide synthesized at the step (a) wherein this the reaction product comprises less 0.05% of sodium (by mass); (c) separation of product synthesized at the step (b) for hydrocarbon phase containing alkylaryl hydroperoxide and an aqueous phase; (d) repeating steps (b) and (c) by one or some time being optionally. Also, synthesis of alkylaryl hydroxide involves the additional treatment step (e) of at least part of hydrocarbon phase containing alkylaryl hydroperoxide synthesized at steps (c) or (d), olefin and a catalyst to yield alkylaryl hydroxide and oxirane compounds, and (f) separation of at least part of oxirane compound from alkylaryl hydroxide. Synthesis of alkenylaryl involves the additional step (g) of dehydration of at least part of alkylaryl hydroxide synthesized at step (f). Invention provides simplifying the technological process resulting to synthesis of improved substance containing alkylaryl hydroperoxide from which alkylaryl hydroxide is prepared followed by preparing alkenylaryl.

EFFECT: improved method of synthesis.

11 cl, 1 tbl, 6 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of styrene. At the first step the method involves interaction of ethylbenzene hydroperoxide with propene in the presence of catalyst to yield propylene oxide and 1-phenylethanol followed by separate treatment of reaction flow and removing propylene oxide. At the second step the method involves interaction of 1-phenylethanol-containing distillate with a heterogenous dehydration catalyst at temperature 150-320°C to obtain styrene. Distillate contains 0.30 wt.-%, not above, compounds of molecular mass at least 195 Da. Invention provides decreasing the content of by-side compounds in styrene and to enhance it's the conversion degree.

EFFECT: improved method of synthesis.

3 cl, 3 tbl

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