Method of obtaining phenol and ketone from hydroperoxide of alkylaromatic hydrocarbon (versions)

FIELD: chemistry.

SUBSTANCE: one of method versions is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification and possibly partial recycling into reaction zone(s) of one or several components of reaction mixture. Decomposition is carried out in presence of inert easily-boiling solvent, which contains mainly hydrocarbons, whose boiling temperature is lower than 70°C, preferably lower than 40°C, but not lower than minus 1°C, which is partially evaporated directly from reaction zone(s) and partially distilled from obtained reaction mixture, is in liquid state returned to reaction zone(s) with supporting in it (them) temperature from 1 to 70°C, preferably from 10 to 45°C. Second method version is carried out in presence of catalyst with strong acidity in one or several reaction zones with further separation of reaction mixture by means of rectification. Applied is easily-boiling solvent, which after separation from reaction mixture, possibly with part of ketone, is recycled into reaction zone(s), and sulfocationite catalyst in H+ form, resistant in liquid media, containing alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons in large amount, at temperatures up to 70°C, in fine-grain or coarse-grain form, possibly, in form of mass-exchange filling with size from 1.5 to 25 mm.

EFFECT: obtaining phenol and ketones without formation of large amount of by-products and resins and practically without equipment corrosion.

14 cl, 1 dwg, 6 ex

 

The invention relates to the field of processing of alkylaromatic hydroperoxides with obtaining phenol and ketones.

Known [M.Kharasch, J.Org.Chem., 1950, 15, R] the method of producing phenol and a ketone, in particular acetone by decomposition of dialkyldimethylammonium in the presence of strong liquid acids. The main disadvantage of this method is the use vysokokorrozivnuyu aggressive catalyst and the absence of an effective technological solution to the problem of removal of the reaction heat (the reaction is highly exothermic).

Known methods [U.S. Pat. US 2661375, 1953, U.S. Pat. Germany 944013, 1956] the process of decomposition of alkylaromatic hydroperoxides with obtaining a phenol and a ketone in the presence of aqueous solutions of sulfuric acid at the contact of two mutually insoluble phases. Disadvantages of these methods is the use vysokokorrozivnuyu aggressive catalyst and the need for special devices for mixing phases.

Known methods of carrying out the process of decomposition of alkylaromatic hydroperoxides with obtaining phenol and ketone when catalyzed with sulfuric acid using homogenizers. In [Ind. Chem., 1960, No. 36, R] as a homogenizer used partially recirculated in the process of phenol. One of the disadvantages of the method is the difficulty of implementing effective heat removal and the presence of side the of aacci phenol.

Was proposed [U.S. Pat. Canada 507550, 1954, U.S. Pat. US 2761877, 1956] and implemented in the manufacturing method for production of phenol and acetone by decomposition of dimethylpolysiloxene in the presence of sulfuric acid, in which a large part of the funds allocated from the reaction mixture of acetone return it in quantities that exceed the number of source hydroperoxide and the formed phenol. Removal of the highly exothermic heat of reaction from the reaction zone a significant portion of the acetone is evaporated, then condense and return to the reaction zone. The method proved to be more effective than the previous one, and is used in industry, including in Russia [Handbook of Neftekhimik, L., Chemistry, 1978, vol. 2, p.184]. The disadvantages of the method are:

- the corrosivity of sulfuric acid and the formation of harmful wastewater with her after neutralization of the reaction zone;

- the formation of large quantities of by-products in the reaction of acetone present in the reaction zone in large quantities and with considerable reaction activity in the presence of an acid catalyst;

- inability to reduce by evaporation of the acetone the reaction zone temperature is below 60°without the use of vacuum, which leads to the formation of by-products: α-methylstyrene and its oligomers, oxide mesityl, is amylphenol and other high-boiling by-products.

We have found ways to obtain the phenol and the ketone decomposition of alkylaromatic hydroperoxides without the formation of high amounts of by-products and resins, as well as virtually no corrosion of equipment.

We say:

Method for production of phenol and a ketone of cumene aromatic hydrocarbon by its decomposition in the presence of a catalyst with strong acidity in one or more reaction zones with subsequent separation of the reaction mixture using distillation and partial recirculation in the reaction(s) area(s) of one or more components of the reaction mixture, characterized in that the decomposition is carried out in the presence of boiling inert solvent, containing predominantly hydrocarbon(s) having a boiling point below 70°C, preferably below 40°but not less than 1°that is partially evaporated directly from the reaction(s) zone(s) and partially distilled off from the obtained reaction mixture, in the liquid state return in the reaction(s) area(s) and maintain it(them) at temperatures ranging from 1 to 70°C, preferably from 10 to 45°C.

As a way conducive to the effective implementation of the method according to claim 1, we declare the methods, characterized in that:

- in the quality or composition of the specified solvent use is predominantly saturated(e) hydrocarbon(s), preferably not containing(e) of the tertiary carbon atoms;

- in the quality or composition specified inert solvent using n-pentane and/or isopentane, and/or cyclopentane, and/or n-butane and/or isobutane;

when the separation of the reaction mixture the solvent allocate by distillation and recycled into the reaction(s) area(s) possibly with a part of the formed ketone content in the recirculated flow limit concentration of not more than 50 wt.%, preferably not more than 25 wt.%;

- hydroperoxide alkylaromatic hydrocarbon, recycled boiling inert solvent and possibly recycled ketone served in the consecutive points of the reaction(s) area(s) two or more streams;

is subjected to decomposition of cumene hydroperoxide and the quality of the products receive phenol and acetone;

is subjected to decomposition of hydroperoxide second-butylbenzene, and as products receive phenol and methyl ethyl ketone;

- when using fine-grained catalyst him ablation prevent restraint(s) device(s) hole size smaller than the minimum size of the catalyst particles.

We also independently declare:

Method for production of phenol and a ketone of the hydroperoxide alkylaromatic hydrocarbon by its decomposition in the presence of a catalyst is and with strong acidity in one or more reaction zones with subsequent separation of the reaction mixture using distillation, characterized in that use boiling solvent, which after separation from the reaction mixture, possibly with part of the ketone, recycle in the reaction(s) area(s), and selfactivity catalyst in H+ form, which is resistant to liquid media containing large quantities of the alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons, at temperatures up to 70°in fine grained or coarse-grained form, perhaps in the form of mass transfer nozzle size from 1.5 to 25 mm

As ways of promoting the effective use of this method, we also declare methods, characterized in that:

- decomposition of the specified hydroperoxide using the specified sulfocationites catalyst is carried out in the presence of boiling inert solvent, containing predominantly hydrocarbon(s) having a boiling point below 70°C, preferably below 40°but not less than 1°S, which is partially evaporated from the reaction(s) area(s) and partially distilled off from the obtained reaction mixture, in the liquid state return in the reaction(s) area(s) and maintain it(them) at temperatures ranging from 1 to 70°C, preferably from 10 to 45°C;

- hydroperoxide alkylaromatic hydrocarbon and recycled boiling inert solvent, possibly ketone, served in th is coherent point of the reaction(s) area(s) two or more streams;

is subjected to decomposition of cumene hydroperoxide, and the quality of the products receive phenol and acetone;

is subjected to decomposition of hydroperoxide second-butylbenzene and quality of products receive phenol and methyl ethyl ketone;

- when using fine-grained sulfocationites catalyst him ablation prevent restraint(s) device(s) hole size smaller than the minimum size of the catalyst particles.

The proposed methods can be used as the inert solvent hydrocarbons with low boiling points, including hydrocarbons4(n-butane, isobutane), hydrocarbons, C5(n-pentane, isopentane, cyclopentane and mixtures thereof and to maintain in the reaction zone sufficiently low temperatures up to +1°With, which reduces the formation of by-products.

As a reactor for the decomposition of alkylaromatic hydroperoxide can be used in the reactors of different types, allowing evaporation of the solvent from the reaction(s) zone(s) and the return of condensate in the reaction(s) area(s), in particular, a straight horizontal (with the vapour space above the liquid), the vertical reactor and/or the reactor with stirring.

Structurally partitioned reactors can be made in the form of multiple separate the reaction apparatus, United by corresponding threads on the steam and liquid phases.

As catalysts it is possible the use of liquid acids in small quantities, however, it is preferable to use porous selfactivity catalysts: coarse (including molded in the form of a mass transfer packing) or fine-grained as you place them in microcontainer with a large number of holes (for example, mesh)or in suspension ("boiling").

If the quality of the raw material mixture of hydroperoxides may decompose hydroperoxides without prior separation, for example the decomposition of the mixture of cumene hydroperoxide and cumene hydroperoxide, sec-butylbenzene (with receipt respectively of phenol and acetone from cumene cumene, phenol and methyl ethyl ketone from cumene second-butylbenzoyl).

The application of the invention illustrated in the drawing and examples. These figures and examples are not preclude the use of other technical solutions under the conditions (s)contained in claim 1 and/or section 5 of the claims.

According to the drawing alkylaromatic hydroperoxide (with admixture of oxygenated alkylaromatic hydrocarbon and possible by-products) comes on line 1. Possible line 2 enters the solution is a strong acid. With the hydroperoxide and possibly what about the acid is mixed completely or partially vaporized stream from the reaction zone R and the condensed solvent (lines 4, 4A). The specified condensate (stream 4) or a mixture (stream 5) are fully or partially directed into the reaction zone R in line 5. Perhaps part of the condensate (stream 4B) and/or part of the acid and/or part of cumene hydroperoxide, line 6 (and later 6A, 6b, 6C) are served in the desired proportions at different points in the reaction zone R. line 3 from the reaction zone R output stream of evaporated solvent (mixture of ketone), which condense and then recycle zone P on line 4.

The reaction zone R has compartments separated by partitions with holes in which are placed (if used) heterogeneous catalyst, in particular suffocation.

From the reaction zone R on line 7 deduce the reaction mixture, which is optionally neutralized apparatus "H" and on line 8 serves in a distillation column K-1. Output the top K-1 steam stream is condensed, and the separator-sump prepare the chin WITH water.

Part of the organic layer, containing mainly solvent, return-1 as phlegmy, and the remaining amount returned in line 10 (hereinafter 10A and 10B may and 10B) in the reaction zone R. the Aqueous layer from the output line 11.

VAT residue K-1 column on line 12 serves in a distillation column K-2. Top K-2 output stream of distillate (mainly containing ketone) in line 13. Further, the thread 13 you who W ill result on lines 13A and/or serves on line 13B to treatment in the node separation of UR.

From below By-2 output stream 14 containing phenol and impurities, which are served in UR site.

The UR site contains several distillation columns, the join order of which may vary. From UR site on line 15 output phenol, line 16 deduce the alkyl benzene (which is preferably recycled to the step of receiving alkylaromatic hydroperoxide), 17 remove heavy impurities. It is also possible from the site of UR output on line 18 ketone (if it was sent in UR cleaning) and output line 19 of the impurities separated from the ketone.

Examples.

In the examples, the concentration specified in % wt.

Example 1.

Processing according to the drawing is subjected to the original stream of cumene hydroperoxide (Hyperize)containing GITARIS-90% (100 kg/h), and isopropylbenzene - 2,5%), acetophenone (1.5%), dimethylphenylcarbinol (DMPC) - 6,0%.

Flow Hyperize mixed with return flow of inert solvent (n-pentane, BP = 36,1°containing ˜21% return acetone (BP = 56,3° (C), and sulfuric acid (catalyst), supplied in an amount such that the concentration of sulfuric acid in the mixture was ˜0,2%. The mixed stream is served by line 5 into the reactor R.

The composition of the mixed stream (organic substances): n-pentane - 62,0%, acetone and 16.2%, GITARIS-19,8%, isopropylbenzene - 0.5%, acetophenone - 0,3%, DMFC is 1.2%. Part acetone pod is t in the reactor R separately.

The reactor R is a horizontal cylindrical tank with baffles ˜ 2/3 height, with holes. In the reactor, maintain the temperature 42°by evaporating part of the solvent (mixed with acetone)condensation and return to the reactor.

In the reactor there is a complete decomposition of Hyperize mainly with the formation of phenol and acetone. From the reactor output 505 kg/h with a mixture of organic substances: n-pentane - 62,0%, acetone - 23,46%, phenol - 12,24%, isopropylbenzene - 0,50%, acetophenone - 0,03%, DMPC - 0,1%, α-methylsterol - 1,05%, the oxide of mesityl to 0.15%, and a small amount of taglocity impurities and water (˜0,2%).

From the K-1 top place and return to the reactor 390 kg/h stream containing 79% of n-pentane and 21% acetone. VAT residue K-1 in the amount of 109 kg/h is fed to the column K-2. From column K-2 top output stream 13 containing mainly acetone, and the bottom is a mixture of high-boiling components.

After the subsequent separation in UR site get ˜61,0 kg/h of phenol and 37.7 kg/h of acetone commodity purity.

Example 2.

Processing according to the drawing is subjected to the original thread Hyperize, the number and composition similar to that specified in example 1 (100 kg/h of Piperita). The content of sulfuric acid in the liquid in the reactor is ˜0,2%.

Unlike example 1 as inert is astorias use n-butane (BP = minus 0.5° C). In the reactor, maintain the concentration of n-butane to 60.6% and temperature of 20°C. the Concentration of Hyperize part of the reactor the flow is 30%. Thus there is a complete decomposition of Hyperize mainly with the formation of phenol and acetone.

From the reactor output 333 kg/h of a mixture containing about 60.6% n-butane, 18.5% phenol, 17.6% of acetone, to 0.75% of cumene, 0,45% of acetophenone, 0,2% DMPC, 1,6% α-methylstyrene, less than 0.01% oxide mesityl, a small number taglocity impurities and water (traces).

From K-1 column is distilled off and returned to the reactor 218 kg/h stream containing 94% n-butane and 6% acetone. From K-2 column distilled 38,0 kg/h almost pure acetone.

When rectification VAT residue column K-1 in UR site get 61.3 kg/h of phenol commodity purity.

Example 3.

Processing according to the drawing is subjected to the original thread Hyperize, the number and composition similar to that specified in example 1 (100 kg/h of Piperita).

As the catalyst in the reactor using fine-grained sulfonation Amberlyst-35 (particle size of 0.4-1.2 mm, static exchange capacity SOY=5,4 mg-ecvn+/g).

In the reactor, maintain the temperature of 65°due to evaporation and subsequent condensation and return of acetone.

The load on the catalyst is 12 kg of liquid mixture per 1 kg of catalyst per hour. At the entrance to the reactor support to the concentrations Hyperize 30-36%, acetone - 60-70%.

From the reactor output 333 kg/h of a mixture containing 77.2% of acetone, 18.6% phenol, 1,55% α-methylstyrene, 0,75% of cumene, 0,80% acetophenone, 0.2% oxide mesityl and ˜0,2% taglocity impurities and water.

From K-1 column distilled, condensed and returned to the reactor 223 kg/h of a stream containing predominantly acetone. Column K-2 is used for the distillation of acetone boiling impurities. The quality of the product output of 37.9% acetone, and the rest recycle to the reactor.

The separation of VAT residue column K-1 in UR site get 61,1 kg/h of phenol commodity purity.

Example 4.

Processing according to the drawing is subjected to the original thread Hyperize, the number and composition similar to that specified in example 1 (100 kg/h of Piperita).

As the catalyst in the reactor using fine-grained sulfonation KU-2-8 emergency (particle size 0.4 to 1.1 mm, the static exchange capacity SOY=4,7 mg-ecvn+/g). As solvent using n-pentane. In the reactor R maintain the concentration of n-pentane ˜52% and a temperature of 44°C. the Concentration of Hyperize at the entrance of the reactor (with respect to the total flow) is 30%. Supply input Hyperize and solvent (mixed with acetone) are distributed between the first three consecutive sections of the reactor in a mass ratio of 4:2:1. The load on the cat is the lyst is 13 kg/h of liquid mixture per 1 kg of catalyst.

From the reactor output 340 kg/h of reaction mixture containing 52,2% of n-pentane, 25.8% of acetone, 18.7% phenol, 0,75% of cumene, 0,77% of acetophenone, 1,4% α-methylstyrene, 0.1 to 0.15% DMPC, 0.1% oxide mesityl and 0.1-0.2% of taglocity impurities and water.

From K-1 column distilled, condensed and returned to the reactor R 215 kg/h stream containing 78% of n-pentane and ˜22% acetone. After rectification VAT residue in the column K-2 and separation in the zone get UR 61,5 kg/h of phenol and 38.3 kg/h of acetone.

Example 5.

Processing according to the drawing is subjected to the original thread Hyperize, the number and composition similar to that specified in example 1 (100 kg/h of Piperita).

As the catalyst in the reactor using a coarse-grained molded selfactivity catalyst KU-FPP (granules in the form of cylinders with a length of 6-10 mm, diameter 4-6 mm, static exchange capacity SOY=3.3V mg-ecvn+/g).

As solvent using n-pentane. In the reactor R maintain the concentration of n-pentane ˜52%, a temperature of 45°C. the Concentration of Hyperize input (relative to the sum of the incoming flows) is 30%.

The load on the catalyst is 4 kg/h per 1 kg of catalyst.

From the reactor output 335 kg/h of reaction mixture containing 51% of n-pentane, 24.7% of acetone, 18.7% phenol, 0,75% of cumene, 0.8% acetophenone, 1,5% α-methylstyrene, 0,2% DMPC, 0.1 to 0.2% oxide mesiti the and and 0.2-0.3% taglocity impurities and water.

From K-1 column distilled, condensed and returned to the reactor 204 kg/h stream containing 79% of n-pentane and ˜21% acetone. After rectification VAT residue in the column K-2 and separation in the zone get UR 61.3 kg/h of phenol and 38,1 kg/h of acetone.

Example 6.

Processing according to the drawing is subjected to the original thread cumene second-butylbenzene (content of 100 kg/h, which is 85% of the flow). The content of other impurities: 2-phenylbutane-2 - 7%, second-butylbenzoyl - 4,0%, ulcerations ketone - 4,0%.

As the catalyst in the reactor using a coarse-grained molded selfactivity catalyst'KEEFE (granules in the form of cylinders with a length of 5-8 mm, diameter 4-6 mm, static exchange capacity SOY=3.6 mg-ecvn+/g).

As solvent using n-pentane. The temperature in the reactor 55°, concenrate hydroperoxide at the entrance to the reactor R (with respect to the sum of the incoming flows) - 30%.

From the reactor output 332 kg/h of reaction mixture containing a 60.2% n-pentane, 17.3% of acetone, 16.9% of phenol, 1,4% of second-butylbenzene, 1.4% of alkylaromatic ketone, 1.8% of 2-phenylbutane-2, 0.5% of 2-phenylbutane-2, and 0.4% taglocity impurities and water.

From K-1 column distilled, condensed and returned to the reactor 215 kg/h of a mixture containing 93% of n-pentane and ˜7% of methyl ethyl ketone.

When rectification VAT residue K-1 column in the column is -2 get 41,5 kg/h of methyl ethyl ketone. The separation of VAT residue column K-2 in the zone get UR 55,5 kg/h of phenol.

1. Method for production of phenol and a ketone of cumene aromatic hydrocarbon by its decomposition in the presence of a catalyst with strong acidity in one or more reaction zones with subsequent separation of the reaction mixture using distillation and partial recirculation in the reaction(s) area(s) of one or more components of the reaction mixture, characterized in that the decomposition is carried out in the presence of boiling inert solvent, containing predominantly hydrocarbon(s) having a boiling point below 70°C, preferably below 40°but not less than 1°that is partially evaporated directly from the reaction(s) zone(s) and partially distilled off from the obtained reaction mixture, in the liquid state return in the reaction(s) area(s) and maintain it(them) at temperatures ranging from 1 to 70°C, preferably from 10 to 45°C.

2. The method according to claim 1, characterized in that the quality or composition of the specified solvent used mainly saturated(e) hydrocarbon(s), preferably not containing(e) tertiary carbon atoms.

3. The method according to claim 1, characterized in that the quality or composition specified inert solvent using n-pentane and/or isopentane, and/and the and cyclopentane, and/or n-butane and/or isobutane.

4. The method according to claim 1, characterized in that the separation of the reaction mixture the solvent allocate by distillation and recycled into the reaction(s) area(s) possibly with a part of the formed ketone content in the recirculated flow limit concentration of not more than 50 wt.%, preferably not more than 25 wt.%.

5. The method according to claim 1, characterized in that hydroperoxide alkylaromatic hydrocarbon, recycled boiling inert solvent and possibly recycled ketone served in the consecutive points of the reaction(s) area(s) two or more threads.

6. The method according to claim 1, characterized in that the decomposition expose of cumene hydroperoxide and the quality of the products receive phenol and acetone.

7. The method according to claim 1, characterized in that the decomposition is subjected to the hydroperoxide second-butylbenzene and quality of products receive phenol and methyl ethyl ketone.

8. The method according to claim 1, characterized in that when using fine-grained catalyst him ablation prevent restraint(s) device(s) hole size smaller than the minimum size of the catalyst particles.

9. Method for production of phenol and a ketone of the hydroperoxide alkylaromatic hydrocarbon by its decomposition in the presence of a catalyst with strong acidity in a single and multiple reaction zones, followed by separation of the reaction mixture using distillation, characterized in that use boiling solvent, which after separation from the reaction mixture, possibly with part of the ketone, recycle in the reaction(s) area(s), and selfactivity catalyst in the N+form, stable in liquid media containing large quantities of the alkylaromatic hydroperoxides, ketones, phenol and hydrocarbons, at temperatures up to 70°in fine grained or coarse-grained form, perhaps in the form of mass transfer nozzle size from 1.5 to 25 mm

10. The method according to claim 9, characterized in that the decomposition of the specified hydroperoxide using the specified sulfocationites catalyst is carried out in the presence of boiling inert solvent, containing predominantly hydrocarbon(s) having a boiling point below 70°C, preferably below 40°but not less than 1°S, which is partially evaporated from the reaction(s) area(s) and partially distilled off from the obtained reaction mixture, in the liquid state return in the reaction(s) area(s) and maintain it(them) temperature from 1 to 70°C, preferably from 10 to 45°C.

11. The method according to claim 9, characterized in that the hydroperoxide alkylaromatic hydrocarbon and recycled boiling inert solvent, possibly ketone, served in the consecutive points of the reaction(s) area(s) two or NESCO is Kimi threads.

12. The method according to claim 9, characterized in that the decomposition expose of cumene hydroperoxide and the quality of the products receive phenol and acetone.

13. The method according to claim 9, characterized in that the decomposition is subjected to the hydroperoxide second-butylbenzene and quality of products receive phenol and methyl ethyl ketone.

14. The method according to claim 9, characterized in that when using fine-grained sulfocationites catalyst him ablation prevent restraint(s) device(s) hole size smaller than the minimum size of the catalyst particles.



 

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2 cl, 4 tbl, 4 ex

FIELD: main organic synthesis.

SUBSTANCE: proposed method is used for production of ketones, for example dimethyl ketone (CH3COCH3), methyl ethyl ketone (CH3COC2H5) by direct catalytic oxidation of respective alkenes, for example propylene, n-butenes, as well as catalysts for realization of this method. Oxidation of alkenes is performed in the presence of metallocomplex catalysts containing organic component where nitrogen oxide (I) is used as oxidant. Used for process is catalyst on base of peroxopolyoxo metallate complexes of terakis (oxo diperoxo metallate)-phosphate (3-) together with quaternary ammonium cationes having formula Q3{PO4[MeO(O2)2]4}, where Me-Mo, W,V; Q3 is quaternary ammonium catione containing alkyl chains C4-C8 or N-hexadecyl pyridinium.

EFFECT: enhanced selectivity of process.

10 cl, 14 ex

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

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

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

5 cl, 4 ex, 8 tbl

FIELD: organic chemistry, in particular production of carbonyl compounds such as aldehydes and ketones.

SUBSTANCE: claimed method includes reaction of nitrous oxide with alkenes in presence of inert gas as diluent. Reaction is carried out in gas phase at 401-700°C and under pressure of 2-300 atm. Target compounds represent value intermediates for precise and base organic synthesis.

EFFECT: method of high selectivity in relation to target products and improved explosion proofing.

5 cl, 1 tbl, 14 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to joint phenol-acetone production via selective decomposition of cumene hydroperoxide. Process is conducted in several in series connected reactors constructed in the form of shell-and-tube heat-exchangers, wherein part of decomposition product is recycled into reaction zone and mixed with feed stream to be decomposed, weight ratio of recycled stream to feed stream being less than 10. Reactors with tubular hydrodynamic characteristic have volumetric heat-exchange surface equal to or larger than 500 m2/m3. Preferably, residual concentration of cumene hydroperoxide is 0.1-0.3 wt % and its residence time in decomposition zone ranges from 0.5 to 10 min.

EFFECT: increased selectivity of decomposition at lesser recycle apparatus volume and reduced investment expenses.

11 cl, 1 dwg, 9 ex

FIELD: chemistry.

SUBSTANCE: H-form of ultrastable dealuminated Y-zeolites HUSY with SiO2/Al2O3 ratio within 5 to 120 is used as catalyst. As a rule, zeolites are combined with a binding agent represented by aluminum oxide, silicon oxide or their mix. Usually the catalyst is preliminarily activated by calcination in air at 300-600°C, while the method is implemented at 20-100°C. As a rule, cumol hydroperoxide concentration in the raw mix varies within 3 to 80%, and acetone, cumol, phenol or their mix with various component ratio are used as solvent.

EFFECT: increased process selectivity in relatively mild conditions.

7 cl, 1 tbl, 11 ex

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