Process of producing styrene via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock (options)

FIELD: industrial organic synthesis.

SUBSTANCE: embodiments of invention are accomplished via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock in presence of acid-type catalyst in column-type reactor-rectifier comprising still portion, built-in heat-exchanger, and rectification portion, volume of still portion constituting 80% of built-in heat-exchanger volume. Temperature of till portion of reactor-rectifier is 140-205°C and temperature in rectification portion 130-180°C. Advantageously, methyl phenyl carbinol-containing feedstock is supplied to and/or under built-in heat-exchanger and catalyst or mixture of catalyst with feedstock and/or still product is supplied to still portion at mixing. Linear velocity of reaction mass vapors within free cross-section of reactor is 0.05 to 0.9 m/s, residence time of styrene in reaction zone 0.05 to 50 sec, and residence time of still product in reactor 5 to 500 h.

EFFECT: increased conversion of feedstock and final product formation selectivity.

5 cl, 14 ex

 

The invention relates to the petrochemical and chemical industries and is designed to produce styrene liquid-phase dehydration of methylphenylcarbinol.

A known method of producing styrene liquid-phase dehydration of methylphenylcarbinol carried out in the reactor dehydration methylphenylcarbinol (IFC) (Testimony of the Russian Federation №23243, IPC701 D 3/14, publ. 06.10.2002). Distillation column, in which the process of dehydration IFC contains at least three theoretical plates, the bottom of the column is connected with a device for heating of the substrate. Raw materials - IFC and the catalyst may act in a device for heating of the substrate. The dehydration reaction proceeds in the device for the heating of the substrate and a bottom part of the column. A pair of reaction products pass through the column plate and are displayed on the condensation. The condensed reaction products enter the sump separation of water and hydrocarbon layers. The hydrocarbon layer is directed to the extraction of styrene, and the water layer for recycling. VAT product is fed for further processing.

The described method does not allow to achieve high conversion IFC because there wasn't enough heat in the reaction zone under conditions endothermic reaction which is the reaction of dehydration of methylphenylcarbinol.

The closest to PR is dliemma invention is a method of producing styrene liquid-phase dehydration of methylphenylcarbinol, carried out in the reactor column type, containing the rectifying part, where the rectifying plate and the distribution plate, built-in heat exchanger type tube below the power lines, and cubic part, equipped with a heat exchange jacket (RF patent for useful model №35600, IPC701 D 3/14, C 07 C 15/46, publ. 27.01.2004). Heated fraction IFC and raw materials for the preparation of the catalyst are served on site preparation of the catalyst. The catalyst enters the lower part of the reactor. Fraction IFC served on a distribution plate of the reactor, passes through a built-in heat exchanger, where it is additionally heated, and gets into a heated outer heat exchange jacket cubic part of the reactor, which is in contact with the catalyst. Formed during dehydration in Cuba reactor, the reaction products evaporate under the influence of temperature and rise in the rectifying part of the reactor, which is separated from the raw material and taglocity impurities by distillation plates. The reaction products from the upper part of the reactor do in the capacitor, and then into a settling tank to separate the oil and water layers. The hydrocarbon layer is applied to the allocation of styrene, and the water layer for further processing. Part of the cubic product is served in recycling, octavas is part of the cubic product is output for further processing.

The disadvantages of this method are the low selectivity and conversion in the process of dehydration IFC due to insufficient heating of a bottom part of the reactor in which the reaction of dehydration IFC.

As catalysts in the process of obtaining styrene liquid-phase dehydration IFC use of acid catalysts, for example amides of sulfuric acid, sulfonic acid, derivatives thereof, and mixtures thereof (patent RF №2132322, IPC607 With 15/46, publ. 27.06.99), sulfuric acid, modified by the introduction of oxygen-containing organic compounds, which are used ketone, alcohol, carboxylic acid, alkalophile, esters on the basis of oxides alkylene and IFC, organic acids and phenols, or sulfuric acid, modified nitrogen-containing compounds such as amines, aminoalcohols, the basis of manniche, hydroxylamine and others (patent RF №2141933, IPC6C 07 C 1/24, 15/46, publ. 27.11.99).

The objective of the invention is to develop ways to achieve high levels of conversion and selectivity in the process of liquid-phase dehydration methylphenylcarbinol raw materials.

The problem is solved by a method of producing styrene liquid-phase dehydration methylphenylcarbinol raw materials in the presence of acid catalyst type reactor rectify the Torah column type, containing cubic part, a built-in heat exchanger and distillation part, the process is carried out in the reactor-rectifier, designed so that the volume of a bottom part of the reactor-rectifier is not more than 80% of the volume of the built-in heat exchanger.

During the process of liquid-phase dehydration methylphenylcarbinol raw material temperature in the bottom part of the reactor-rectifier withstand 140-205°C, and the temperature in the rectifying section of the reactor-rectifier - 130-180°C.

Filing methylphenylcarbinol raw materials can be done with built-in heat exchanger of the reactor-rectifier and/or underneath it.

The flow of catalyst or mixture of catalysts with methylphenylcarbinol raw materials and/or kubovy product can be done in cubic part of the reactor-rectifier when mixed.

The method of producing styrene liquid-phase dehydration methylphenylcarbinol raw materials in the presence of acid catalyst of the type carried out in the reactor-rectifier column type, containing cubic part, a built-in heat exchanger and distillation part, and the process is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor of 0.05-0.9 m/s, the residence time of the styrene in the reaction zone of 0.05-50 with a time of CC about the ukta in the reactor 5-400 PM

The difference between the proposed methods for producing styrene is that the process is carried out in the reactor-rectifier, designed so that the volume of a bottom part of the reactor-rectifier is not more than 80% of the volume integrated heat exchanger, when the process temperature at a bottom part of the reactor-rectifier withstand 140-205°C, and the temperature in the rectifying section of the reactor-rectifier - 130-180°and that the supply methylphenylene-nasteride raw materials can be done with built-in heat exchanger of the reactor-rectifier and/or under it, and the flow of catalyst or a mixture of the catalyst methylphenylcarbinol raw materials and/or kubovy product is in the cubic part of the reactor-rectifier when mixed.

In addition, during the process of liquid-phase dehydration methylphenylcarbinol raw linear velocity of vapors of the reaction mass in the free cross section of the reactor is 0.05 to 0.9 m/s, the residence time of the styrene in the reaction zone of 0.05-50, time the cubic product in the reactor 5-400 PM

As methylphenylcarbinol raw materials can be used, for example, the fraction IFC co-production of propylene oxide and styrene, and any other fraction containing IFC.

As the acid catalyst type can be used, n is the sample, amide sulfuric acid, sulfonic acid amide, derivatives thereof, and mixtures thereof, or sulfuric acid, modified by the introduction of oxygen-containing organic compounds and/or nitrogen-containing compounds, or phosphorus and/or organic acid, modified additives oxygen and/or nitrogen-containing compounds, or any other known acid catalyst type. The catalyst may be used in the form of solutions, or suspensions or emulsions.

The reactor-rectifier, in which the process of liquid-phase dehydration methylphenylcarbinol raw materials, can have a plate of any structures or bulk head. The upper limit of the number of theoretical plates is limited to economic feasibility, and temperature necessary to maintain the reaction medium in the liquid state.

In accordance with the invention the process of liquid-phase dehydration methylphenylcarbinol raw materials is as follows.

The process of liquid-phase dehydration methylphenylcarbinol raw materials is carried out in the reactor-rectifier column type, containing cubic part, equipped with a heated device, a built-in heat exchanger and distillation part. The volume of a bottom part of the reactor-rectifier is not b is over 80% of the volume integrated heat exchanger. Methylphenylcarbinol raw material, heated to a temperature of 120-140°served on the built-in heat exchanger of the reactor-rectifier column type and/or under it, the catalyst or the mixture of the catalyst methylphenobarbital raw materials and/or kubovy product is served in the cubic part of the reactor-rectifier by mixing, for example, via a pump or mixer of any design. The process of dehydration proceeds in a bottom part of the reactor-rectifier at a temperature 140-205°C. a Pair of reaction products obtained in the bottom part of the reactor-rectifier in the reaction of dehydration methylphenylcarbinol raw materials, through the built-in heat exchanger, are a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

The process of liquid-phase dehydration methylphenylcarbinol raw materials is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor of 0.05-0.9 m/s, the residence time of the styrene in the reaction zone of 0.05-50 C and the residence time of the cubic product in the reactor 5-400 PM

After distillation of the reactor-rectifier with a temperature of 130-180°With, a pair of reaction products are naweglanie styrene known methods. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The implementation of the present invention are illustrated in the following examples.

Example 1

The process is carried out in the reactor-rectifier column type, containing cubic part, equipped with a heat exchange jacket, built-in heat exchanger and distillation part. The volume of a bottom part of the reactor-rectifier 60% of the volume integrated heat exchanger. Fraction IFC co-production of propylene oxide and styrene having the following composition, wt.%: ∑ boiling hydrocarbons 0,01; benzaldehyde 0,02; acetophenone (ACP) 13,69; IFC 82,47; magelonidae hydrocarbons 3,81, heated to a temperature of 120°With, in the amount of 22011,21 kg/h serves on the built-in heat exchanger of the reactor-rectifier column type, the catalyst is sulfuric acid at a fraction of the IFC in the amount of 2321,33 kg/h is fed into the cubic part of the reactor-rectifier under intensive mixing by the mixer. The process of dehydration proceeds in a bottom part of the reactor-rectifier at a temperature of 140°C. a Pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, are a distillation of the reactor-rectifier, in which occurs the separation of styrene, water spray other boiling components from acetophenone, IFC and other components with a higher boiling point.

After distillation of the reactor-rectifier with a temperature of 130°With, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 24089,21 kg/h containing 68,84 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 89.1%, and conversion - 95.3 per cent.

Example 2

The process is carried out in the reactor-rectifier column type, the volume of a bottom part which is 80% of the volume integrated heat exchanger. Fraction IFC co-production of propylene oxide and styrene, of the same composition and in the same amount as in example 1, serves on the built-in heat exchanger of the reactor-rectifier, the catalyst is sulfuric acid at a fraction of the IFC in the amount of 1500 kg/h is fed into the cubic part of the reactor-rectifier under intensive mixing by means of the pump. The process of dehydration proceeds in a bottom part of the reactor-rectifier at a temperature of 205°C. a Pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, are a distillation of the reactor-rectifier, in which p is oshodi Department of styrene, water and other boiling components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier with a temperature of 180°With, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 22715,15 kg/h containing 70,54 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 99.9%, the conversion - 99,95%.

Example 3

The process is carried out in the reactor-rectifier column type, the volume of a bottom part which is 80% of the volume integrated heat exchanger. Fraction IFC co-production of propylene oxide and styrene, of the same composition and in the same amount as in example 1, served by a built-in heat exchanger of the reactor-rectifier, the catalyst is sulfuric acid at a fraction of the IFC in the amount of 1000 kg/h is fed into the cubic part of the reactor-rectifier under intensive mixing by means of the pump. The process of dehydration proceeds in a bottom part of the reactor-rectifier at a temperature of 205°C. a Pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, proceed in re tification part of the reactor-rectifier, in which there is a division of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier with a temperature of 180°With, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 22454,91 kg/h containing 69,84 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 99.99%, conversion of 98.3%.

Example 4

The process is carried out in the reactor-rectifier column type, the volume of a bottom part of which does not exceed the built-in heat exchanger. Fraction IFC co-production of propylene oxide and styrene, of the same composition and in the same amount as in example 1, served by a built-in heat exchanger of the reactor-rectifier, the catalyst is sulfuric acid at a fraction of the IFC in the amount of 2300 kg/h is fed into the cubic part of the reactor-rectifier under intensive mixing by means of the pump. The process of dehydration proceeds in a bottom part of the reactor-rectifier at a temperature of 140°C. a Pair of reaction products obtained in the bottom part of the reactor-rectifier, passing through built-in the built-in heat exchanger comes in a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier with a temperature of 130°With, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 21375,92 kg/h containing 77,51 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 94,86%, conversion - 99,73%.

Example 5

The process is carried out in the reactor-rectifier column type, containing cubic part, equipped with a heat exchange jacket, built-in heat exchanger and distillation part. Fraction IFC co-production of propylene oxide and styrene having the following composition, wt.%: ∑ boiling hydrocarbons 0,01; benzaldehyde 0,02; acetophenone (ACP) 13,69; IFC 82,47; magelonidae hydrocarbons 3,81, heated to a temperature of 130°With, in the amount of 22011,21 kg/h and the catalyst is sulfuric acid at a fraction of the IFC in the amount of 1934,4 kg/h is fed into the reactor-rectifier column type.

The process of liquid-phase dehydration of METALFORCE inasteride raw materials is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor 0.05 m/s, time for the presence of styrene in the reaction zone 50 and the time spent by the cubic product in the reactor 5 hours

A pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, are a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 21759,09 kg/h containing 75 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is to 98.4%, conversion of 99.9%.

Example 6

The process is carried out in the reactor-rectifier column type, containing cubic part, equipped with a heat exchange jacket, built-in heat exchanger and distillation part. Fraction IFC co-production of propylene oxide and styrene having the following composition, wt.%: ∑ boiling hydrocarbons 0,01; benzaldehyde 0,02; acetophenone (ACP) 13,69; IFC 82,47; magelonidae hydrocarbons 3,81, heated to a temperature of 120�B0; Since, in the amount of 16,000 kg/h and the catalyst is sulfuric acid at a fraction of the IFC, which added to the basis of manniche, in the amount of 1100 kg/h fed into the reactor-rectifier column type.

The process of liquid-phase dehydration methylphenylcarbinol raw materials is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor 0.9 m/s, the residence time of the styrene in the reaction zone 0.05 s and the residence time of the cubic product in the reactor 400 hours

A pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, are a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 16865,3 kg/h containing 70,1 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 98.8%, conversion - 99,6%.

Example 7

The process is carried out in the reactor-rectifier column type, the content is Adam cubic part, equipped with a heat exchange jacket, built-in heat exchanger and distillation part. Fraction IFC co-production of propylene oxide and styrene having the following composition, wt.%: ∑ boiling hydrocarbons 0,01; benzaldehyde 0,02; acetophenone (ACP) 13,69; IFC 82,47; magelonidae hydrocarbons 3,81, heated to a temperature of 120°With, in the amount of 10000 kg/h and the catalyst is sulfuric acid at a fraction of the IFC containing definititely ether and monoethanolamine, in the amount of 155 kg/h fed into the reactor-rectifier column type.

The process of liquid-phase dehydration methylphenylcarbinol raw materials is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor of 0.5 m/s, the residence time of the styrene in the reaction zone 20 and the time spent by the cubic product in the reactor 200 hours

A pair of reaction products obtained in the bottom part of the reactor-rectifier, through a built-in heat exchanger, are a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier, a pair of reaction products are fed to the allocation of styrene known methods. As the upper productfeature-rectifier selected product number 8566,76 kg/h, containing 78,4 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process is 99,3%, the conversion of 99.8 per cent.

Example 8

The process is carried out in the reactor-rectifier column type, containing cubic part, equipped with a heat exchange jacket, built-in heat exchanger and distillation part. Fraction IFC co-production of propylene oxide and styrene having the following composition, wt.%: ∑ boiling hydrocarbons 0,01; benzaldehyde 0,02; acetophenone (ACP) 13,69; IFC 82,47; magelonidae hydrocarbons 3,81, heated to a temperature of 120°served in the reactor in two streams. The first thread in the amount of 5000 kg/h serves on the upper tubular grille built-in heat exchanger of the reactor. A second thread in the amount of 5000 kg/h with dissolved catalyst is sulfuric acid with the addition of monoethanolamine and diphenyldisulfide ether - served in the cubic part of the reactor.

The process of liquid-phase dehydration methylphenylcarbinol raw materials is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor of 0.5 m/s, the residence time of the styrene in the reaction zone 20 and the time spent by the cubic product in the reactor 200 hours

A pair of reaction products obtained in the bottom part of the reactor-rectifier, PR is walking through the built-in heat exchanger, comes in a distillation of the reactor-rectifier, in which occurs the separation of styrene, boiling water and other components from acetophenone, IFC, and other components with a higher boiling point.

After distillation of the reactor-rectifier, a pair of reaction products are fed to the allocation of styrene known methods. As the top product of the reactor-rectifier selected product number 8565,4 kg/h containing 78,6 wt.% styrene. Part of the bottom liquid of the reactor-rectifier goes to recycling, the part for further processing.

The selectivity of the process was 99.4%, the conversion of 99.9%.

Example 9

The process is carried out as in example 8.

Fraction IFC co-production of propylene oxide and styrene serves as two flows of 5000 kg/h of the First stream is served on the upper tubular grille built-in heat exchanger of the reactor, and the second thread are served in the cubic part of the reactor. The catalyst is concentrated sulfuric acid is served in the cubic part of the reactor.

Thus the selectivity of the process is 97,6%, the conversion rate is 95.8%.

Example 10

The process is carried out as in example 8.

Fraction IFC co-production of propylene oxide and styrene served in the quantity of 10000 kg/h, and the catalyst after its preliminary mixing with the mass contained in a bottom part of the reactor, served under the lower tubular grille built-in heat exchanger of the reactor.

The selectivity of the process is 95.4%, conversion - 94,9%.

Example 11

The process is carried out as in example 8.

Fraction IFC co-production of propylene oxide and styrene served in the quantity of 10000 kg/h, and the catalyst after its preliminary mixing with the faction IFC and the mass contained in a bottom part of the reactor, served under the lower tubular grille built-in heat exchanger of the reactor.

The selectivity of the process is 94,9%, conversion of 94.5%.

Example 12

The process is carried out as in example 3. The volume of a bottom part of the reactor rectifier is 90% of the volume of the built-in heat exchanger.

The selectivity of the process is 94,1%, the conversion of 97.8%.

Example 13

The process is carried out as in example 3. The volume of a bottom part of the reactor rectifier is 110% of the volume of the built-in heat exchanger.

The selectivity of the process is 91.4%, while the conversion rate of 92.9%.

Example 14

The process is carried out as in example 3. The volume of a bottom part of the reactor rectifier is 150% of the volume of the built-in heat exchanger.

The selectivity of the process is the 87.3%, the conversion rate of 83.6%.

Thus, as examples 12-14, the increase in bottom part of more than 100% compared with the volume of the tubular part of the reactor PR which leads to the deterioration process.

As seen from the above examples, the present invention allows to achieve high levels of conversion and selectivity in the process of liquid-phase dehydration methylphenylcarbinol raw materials in the presence of acid catalyst type.

1. The method of producing styrene liquid-phase dehydration methylphenylcarbinol raw materials in the presence of acid catalyst type reactor-rectifier column type, containing cubic part, a built-in heat exchanger and distillation portion, wherein the process is carried out in the reactor-rectifier, designed so that the volume of a bottom part of the reactor-rectifier is not more than 80% of the volume of the built-in heat exchanger.

2. The method of producing styrene according to claim 1, characterized in that the temperature in the bottom part of the reactor-rectifier withstand 140-205°C, and the temperature in the rectifying section of the reactor-rectifier - 130-180°C.

3. The method of producing styrene according to claim 1, characterized in that the supply of methylphenylcarbinol raw materials is carried out on the built-in heat exchanger and/or below a built-in heat exchanger of the reactor-rectifier.

4. The method of producing styrene according to claim 1, characterized in that the flow of catalyst or mixture of catalysts with methylphenylcarbinol raw materials and/or kubovy product ASU is estlat in cubic part of the reactor-rectifier when mixed.

5. The method of producing styrene liquid-phase dehydration methylphenylcarbinol raw materials in the presence of acid catalyst type reactor-rectifier column type, containing cubic part, a built-in heat exchanger and distillation portion, wherein the process is carried out at a linear velocity of the vapors of the reaction mass in the free cross section of the reactor of 0.05-0.9 m/s, the residence time of the styrene in the reaction zone of 0.05-50 C and the residence time of the cubic product in the reactor 5-400 PM



 

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FIELD: industrial organic synthesis.

SUBSTANCE: embodiments of invention are accomplished via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock in presence of acid-type catalyst in column-type reactor-rectifier comprising still portion, built-in heat-exchanger, and rectification portion, volume of still portion constituting 80% of built-in heat-exchanger volume. Temperature of till portion of reactor-rectifier is 140-205°C and temperature in rectification portion 130-180°C. Advantageously, methyl phenyl carbinol-containing feedstock is supplied to and/or under built-in heat-exchanger and catalyst or mixture of catalyst with feedstock and/or still product is supplied to still portion at mixing. Linear velocity of reaction mass vapors within free cross-section of reactor is 0.05 to 0.9 m/s, residence time of styrene in reaction zone 0.05 to 50 sec, and residence time of still product in reactor 5 to 500 h.

EFFECT: increased conversion of feedstock and final product formation selectivity.

5 cl, 14 ex

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: industrial organic synthesis and catalysts.

SUBSTANCE: invention provides a method for processing methanol into dimethyl ether and liquid hydrocarbons, the latter being used as high-octane components of gasolines Ai-92, 95. Processing comprises contacting of raw material, in at least one step, in at least one reactor containing catalyst: Pentasil-type zeolite and binder, followed by cooling resulting products, condensation and separation thereof to isolate methanol conversion hydrocarbon gases, water, and desired products, after which cooled hydrocarbon gases are recycled to methanol conversion stage in at least one reactor. Catalyst is characterized by SiO2/Al2O3 molar ratio 20-100, content of sodium oxide not higher than 0.2%, and additionally contained silicon dioxide and zirconium dioxide at following proportions of components: 1.0-15.0% silicon dioxide, 1.0-5.0% zirconium dioxide, 20-70% zeolite, and binder - the balance.

EFFECT: increased yield of desired products and improved performance characteristics of catalyst.

4 cl, 5 tbl, 18 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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