Method for processing of phenolic resins

 

(57) Abstract:

Usage: recycling co-production of phenol and acetone Kukolnik method, hydrocracking and hydrogenation of phenolic resin in the solvent environment. The inventive phenolic resin is mixed with cumene or a hydrogenation product output from the final stage of this process, the volume ratio of 1 : 1 and the mixture is then subjected to hydrocracking in the presence of hydrogen and of a catalyst containing crystalline miniserial, composition, wt.%: CoO 5; MoO315; miniserial 10; Al2O3the rest of it. The resulting hydrogenation product additionally hydronaut on the catalyst composition, wt.%: Pd of 0.5; the aluminosilicate containing 10% zeolite. The hydrocracking is carried out at 320 - 380oC pressure 3 - 4 MPa, with the supply of raw materials 3 - 4 h-1when the ratio of hydrogen : raw 1000 - 1200 : 1 l/L. the Hydrogenation products of the hydrocracking is carried out at 100 - 250oC, pressure 3 - 4 MPa, flow rate of 1.5 - 2 h-1, the ratio of hydrogen : raw 1000 - 1200 : 1 l/l 1 C.p. f-crystals, 1 table.

The invention relates to organic catalytic chemistry, in particular to a method for producing phenol and cumene from phenolic resin, and can be used in not achieved the effect, the production of phenol and cumene from phenolic resin by hydroperiod at T 350 385oC, Vc1,0 1,2 h-1P 5 7 MPa, the ratio of H2raw materials 1 800 l/l in the presence of alumocobalt catalyst (VRTU 541-57) composition, wt. CoO 6,5 Moo313,5; -Al2O3the rest of it.

Method (1) allows, under specified conditions from the original resin containing 30.5% of IPA, 12% phenol, and 9.5% complex phenol, 15% resin, 3% a-methyl-styrene, 18% of acetophenone, other hydrocarbons rest up to 100% to obtain a hydrogenation product containing 39,8% IPA, 16.8% of ethylbenzene, 17.7% of phenol, and 11.2% resins, other hydrocarbons of the paraffin series to 100% of the rest.

Method (1) has the following disadvantages.

1. The low growth rate of phenol in the hydrogenation product in relation to the original resin, which is 6% and IPA 9.5% in the same time as ethylbenzene increased by 17%

2. The low degree of conversion in the hydrogenation of resinous compounds, which does not exceed 25% of the hydrogenation product is black with the actual resin content of 11.2% (in the feedstock, 14,55%), color more than 8 units on the WTC.

3. Mainegenealogy the period of operation of the catalyst does not exceed 600 hours

4. The total conversion in the hydrogenation of phenol resin is 75 - 80%

The purpose of the image is public phenol and isopropylbenzene (cumene).

The objective is achieved by the fact that the original phenolic resin mixed with IPA or a hydrogenation product with a volumetric ratio of 1 to 1 is subjected to hydrocracking at T 320 385oC R 3 4 MPa, Vc3 4 h-1, the ratio of H2raw 1000 1200 1 l/l in the presence of a catalyst composition, wt. Soo 5; Moo315; MgSi 10; g-Al2O3else, the products of hydrocracking component phenolic resin additionally hereroense on the catalyst composition, wt. Pd 0,5, aluminosilicate, containing 10% zeolite REE, the rest to 100% at T 100 250oC, Vc1,5 2,0 h-1R 3 4 MPa, H2raw 1000 1200 1 l/l

Process for the proposed method allows to obtain a phenolic resin hydrogenation product containing 20 to 25% phenol, 22 35% IPA with a low content of alpha-methylstyrene and resins.

The hydrogenation product after hydrobromide phenolic resin mixed with IPA containing 38.5% of IPA, and 2% phenol, 19% complex phenol, 2,1% ACF, 11.4% of dimers of alpha-methylstyrene, 25% heavy resins, the rest DMFC etc. contains 4 4.8% benzene, 62 64% IPA, 19 of 20% phenol, 0,13 0,2% ACF, 0,9 2,6% heavy paraffin + naphthenes, and other 10 12%

The hydrocracking catalyst is prepared as follows: the precipitate of aluminum hydroxide c Na2O not more than 0.1% with a moisture content of 78 to 82% in kneading m the next type crystalline salt of molybdenum, nitrate of cobalt, weight pariveda to a moisture content of 50 to 55% is formed into extrudates by screw extrusion granulator with a diameter of 2 to 5 mm, the granules are dried, prokalyvayutsya at 550oC.

The catalyst (ball) for the hydrogenation products of hydrocracking and neprivrednih unsaturated compounds is prepared as follows: ball-alumina carrier containing: 90% SiO2, 8% Al2O3and 8% to 10% zeolite REE, is impregnated with a solution of palladium chloride, is recovered 1.5 to 3% solution of formic acid and/or hydrogen peroxide, and the catalyst is dried at 100 to 120oC for 10 12 hours

To date the literature has not been described methods for producing phenol and cumene from phenolic resin using the above catalyst composition, and therefore it can be argued that the claimed combination of features of an object is new and, therefore, the corresponding solution has criterial feature of the "novelty."

On the other hand, the distinctive features of the proposed technical solutions (way) from the well-known are the following.

1. The application of the new aluminoborosilicate (AKM) catalyst and providei hydrogenation products of hydrocracking, resins, alpha-methylstyrene and other unsaturated hydrogen hydrocarbons at low temperature on palladium alyumosilikoklasticheskie catalyst.

Based on the above characteristics, we can say that the essence of the proposed facility is not obvious from the well-known in the industry prior art, therefore, it has criterial element of the invention "inventive step".

Technologically, the proposed method can be implemented in the chemical and petrochemical industry and can be obtained from phenolic resins - waste production of phenol and acetone hydrogenation product containing 20 to 25% phenol, 22 35% of cumene with low content of alpha-methylstyrene and resins. Therefore, our object has the third criterion a symptom of the invention "industrial applicability".

Example 1.

Raw mixture of phenolic resin and cumene in a volume ratio 1 1 according to table is subjected to hydrocracking catalyst composition, wt. CoO 5; MoO315; magnesium-silicate 10; g-Al2O370, 320oC, P 3 MPa, Vc3 h-1, the ratio of H2raw 1000 1 l/l products UB> 1.5 h-1, the ratio of H2raw 1000 1 l/L. the Results obtained in example 1 and subsequent examples, presented in the table.

Example 2.

The process is carried out on raw materials in example 1, the catalyst composition of example 1, hydrocracking at 380oC, Vc4 h-1P 4 MPa, the ratio of H2raw materials 1200 1 l/l, additional hydrogenation at 250oC, Vc2 h-1P 4 MPa, the ratio of H21200 1 l/l

Example 3.

The process is carried out on raw materials in example 1, the catalyst composition of example 1, hydrocracking at 350oC; Vc3.5 h-1R 3.5 MPa, the ratio of H2raw 1100 l/l, the addition of the hydrogenation at 175oC, Vc1.7 h-1P 3.5 MPa, the ratio of H2raw 1100 1 l/l

Example 4 (for comparison).

The process is carried out on raw materials in example 1, the catalyst composition of example 1, hydrocracking at 310oC, Vc2.5 h-1; P 2.5 MPa, the ratio of H2raw 900 1 l/l, hydrogenation in the 90oC, Vc1,3 h-1P 2.5 MPa, the ratio of H2raw 900 l/l

Example 5 (for comparison).

The process is carried out on raw materials in example 1, the catalyst composition of example 1, hydrocracking at 390oC, VcSUB> 2.5 h-1; P 4.5 MPa, the ratio of H2raw 1300 1 l/l

Example 6 (comparison).

The process is conducted as in example 1, but the catalyst for hydrocracking, not containing magnicient.

Example 7 (for comparison).

The process is conducted according to example 1, however, additional hydrogenation is omitted.

Example 8 (comparison).

The process is carried out on raw materials in example 1, the hydrogenation catalyst composition of example 1, however, the preliminary hydrocracking feedstock is omitted.

As can be seen from the data table, the method of examples 1 to 3 compared to 4 to 8 and the prototype provides the receive section of hydrogenated feed with 100% yield and content of phenol 17,2 25% IPA 59,1 64,0% paraffin-naphthene hydrocarbons 8,8 11,4% (a component of gasoline) at a low content of heavy, dimer a-m-styrene complex phenol, acetophenone. It also shows that the reaction product as compared with the raw material has a lower (188 192oC) the temperature of the end of the boil; the resulting hydrogenation product is compared with raw color 0,5 1,0% CNT instead of 8% for the raw mix.

The catalysts in the process according to example 1 of the 3 work stably without regeneration 1000 hours

Example 9. The process is performed on the catalyst and conditions described in example 3. As raw materials use of phenolic resin with the hydrogenation product in the ratio of 1 to 1. Blending is used, the hydrogenation product obtained in the process described in example 3, the following composition, wt. arena C6- C84,3; IPA 59,1; paraffin-naphthene hydrocarbons 10,1; phenol 24,7; alpha methylsterol 0,9; complex phenol 0.1; acetophenone 0,2; dimer of alpha-methylstyrene 0,1.

The reaction product compared to the raw material has a lower temperature at the beginning and end of the boil, 1.5 times higher phenol content than the product obtained according to example 3, color 0,5 1,0% CNT, instead of 8% for the initial mixture.

The catalysts in the process of work stably without regeneration 1000 h, as in example 1, 3.

Example 10.

The process is conducted according to example 2, but instead of cumene take the hydrogenation product obtained in example 2 (composition see table).

The resulting product has a color 0,5 1,0% CNT, on the fractional composition differs little from the composition in example 2, the content of phenol on 17,85% higher UPS and 13% lower than the hydrogenation product from example 2.

Example 11.

The process is conducted as in example 1, where instead of IPA taken is 13% lower than in the hydrogenation product obtained in example 1 (see table).

As can be seen from the table data, the use during processing of phenolic resin for dilution hydrogenates allows to obtain a higher content of phenol in the range of 33 to 38% than in the case of dilution resin cumene content of phenol is 17 25%

1. Method for processing of phenolic resins, including hydrocracking at elevated temperature and pressure in the presence of hydrogen and of a catalyst containing the oxides of cobalt, molybdenum, aluminum, characterized in that the phenolic resin is mixed with cumene or a hydrogenation product obtained at the final stage of the proposed method and having in its composition of phenol 17 25% of cumene 60 to 65% of alpha-methylstyrene to 1.5% and with low content of resin in a volume ratio of 1 to 1 and the hydrocracking is carried out with a catalyst, optionally containing crystalline miniserial, composition, wt. CoO 5, MoO315, miniserial 10, gamma-Al2O3else, then the resulting product is additionally hydronaut over a zeolite catalyst containing 0.5 wt. palladium.

2. The method according to p. 1, wherein the hydrocracking is carried out at 320 - 380oWith, ut at 100 250oWith 3 to 4 MPa, the space velocity of the raw material 1,5 2,0 h-1and at a flow rate of hydrogen 1000 1200 l per 1 l of raw materials at every stage of the process.

 

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FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to manufacturing phenol by cumene method, in particular, to a step for treatment of final product and preparing phenol of high purity degree. Method for treatment of crude phenol is carried out for two steps. At the first step method involves oxidation of acetol, aldehydes and α-methylstyrene with air oxygen in phenol medium by using a heterogeneous catalyst comprising metals with transient valence. At the second step method involves condensation of oxidation products and non-oxidized products by using a heterogeneous acid catalyst. Separation of compounds in the process of phenol treatment is carried out on the final step of isolation of the commercial product by distillation method. At the first stage metal compounds of by-side subgroups 1 and 6 and metals of 8 group of Periodic system on neutral or acid carrier are used as a catalyst preferably. At the second step alumosilicate contacts based on zeolites of type "X" or "Y", or other zeolites comprising or not comprising promoting and modifying additives are used as a catalyst. Invention provides the high degree of purification of phenol from impurities and the improvement of economy indices of the process.

EFFECT: improved method for phenol treatment.

12 cl, 5 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing bisphenol A, which is a starting compound in producing epoxy or polycarbonate resin, involving: (A) a condensation reaction step, involving a reaction between acetone and excess phenol in the presence of an acid catalyst, (B) a concentration step, involving concentration of the reaction mixture obtained at the condensation reaction step, (C) a step for crystallisation and separation of solid/liquid phases, involving crystallisation of an adduct of bisphenol A and phenol by cooling the concentrated liquid obtained at the concentration step, and separation of the concentrated liquid into an adduct and mother liquid, (D) an isomerisation step, involving isomerisation of bis(hydroxyphenyl)propanes, different from bisphenol A, into bisphenol A, carried out by bringing all the mother liquid obtained at the step for crystallisation separation of the solid/liquid phases into contact with a strongly acidic cation-exchange resin, (E) an extraction step involving feeding through a circulation loop a portion of the isomerised liquid back to at least one step selected from (A) a condensation reaction step, (B) a concentration step and (C) a step for crystallisation and separation of the solid/liquid phases, while simultaneously extracting bisphenol A and phenol from the portion of the isomerised liquid, (F) an adduct decomposition step, involving removal of phenol from the adduct of bisphenol A and phenol and extraction of bisphenol A and (G) a granulation step, involving granulation of bisphenol A obtained at the adduct decomposition step. Concentration of water in the mother liquid, which contains bis(hydroxyphenyl)propanes, at the isomerisation step (D) is controlled by keeping it in the 0.2-0.9 wt % range.

EFFECT: method enables to prolong the service life of an isomerisation catalyst and efficiently obtain the desired product.

2 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to versions of a method of producing bisphenol A, one of which comprises a step for removing free acid using a resin selected from strongly acidic ion-exchange resin, strongly basic ion-exchange resin, weakly basic ion-exchange resin and mixture thereof, at the next step (D) in order to remove the remove free acid contained in the mother liquid or isomerised liquid, wherein the method of producing bisphenol A involves: a condensation reaction step (A), on which excess amount of phenol reacts with acetone in the presence of an acid catalyst; a concentration step (B) on which the reaction mixture obtained at step (A) is concentrated; a step for crystallisation or separation of the solid phase and liquid phase (C) on which the adduct of bisphenol A and phenol is crystallised by cooling the concentrated reaction mixture obtained at step (B), and that adduct is separated from the mother liquid; an isomerisation step (D) on which the entire mother liquid obtained at step (C) is isomerised using an isomerisation catalyst and the obtained isomerised liquid is returned to step (A) and/or step (B); a step for decomposition of the adduct (F), on which molten bisphenol A is obtained by removing phenol from the adduct of bisphenol A and phenol obtained at step (C); and a granulation step (G) on which a granular product is obtained by granulating the bisphehol A melt obtained at step (F). The invention also relates to versions of apparatus for implementing the said method.

EFFECT: high efficiency of the method.

10 cl, 4 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to the process for conversion of by-products during the synthesis of bisphenol A. The proposed method consists in the following: the solution of by-products and p, p'-BPA in phenol containing not more than 18% isomer p, p'-BPA, no more than 0.5% of water and not less than 0.15 mol of isomer o, p'-BPA per 1 mole of p, p'-BPA and at least 0.01 mol of trisphenols per 1 mol of p,p'-BPA, is contacted at a temperature of at least 60°C to 80°C as well as at volume and spatial flow rate of up to 2.0 m3/(m3k·hour) with macroporous sulfonion-exchange resin in the hydrogen form ion with a bimodal structure and the total volume of pores having a radius of not more than 20 nm in the resin is less than 0.5 ml/g, whereas the total volume of pores with a radius of 20 nm - 100 nm is greater than 0.8 ml/g.

EFFECT: invention allows to improve the conversion of by-products in the synthesis of bisphenol A aimed to isomer p,p'-BPA, and also aimed to limiting the number of obtained undesirable by-products.

5 cl, 2 tbl, 16 ex

FIELD: organic chemistry, medicine, pharmacy.

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

EFFECT: valuable medicinal properties of compounds.

13 cl, 2 tbl, 2 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to production of phenol via acid catalytic decomposition of cumene hydroperoxide followed by isolation of phenol from decomposition products and purification of phenol to remove trace impurities including acetol. Purification of phenol is accomplished through hetero-azeotropic rectification with water. Acetol is isolated as a part of liquid-phase side stream from semiblind plate located within exhausting section of hetero-azeotropic rectification column. Side stream is supplemented by cumene and used to supply stripping column, from which fraction of acetol/cumene azeotropic mixture is taken as distillate and residue is returned under semiblind plate of hetero-azeotropic rectification column to be further exhausted. From the bottom of the latter, crude phenol is withdrawn and passed to final purification from the rest of reactive trace impurities. Acetol/cumene azeotropic mixture is subjected to heat treatment at 310-350°C, which may be performed in mixtures with high-boiling production waste or in mixtures with bottom product of rectification column for thermal degradation of high-boiling synthesis by-products, which bottom product is recycled via tubular furnace. Above-mentioned semiblind plate, from which side stream is tapped, is disposed in column zone, wherein content of water is minimal and below which contact devices are positioned with efficiency at least 7.5 theoretical plates. Side stream with cumene added to it is passed to the vat of stripping column with efficiency at least 15 theoretical plates.

EFFECT: minimized content of acetol in purified phenol and reduced power consumption.

5 cl, 3 dwg, 6 tbl, 4 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: organic chemistry, chemical technology.

SUBSTANCE: invention relates to manufacturing phenol by cumene method, in particular, to a step for treatment of final product and preparing phenol of high purity degree. Method for treatment of crude phenol is carried out for two steps. At the first step method involves oxidation of acetol, aldehydes and α-methylstyrene with air oxygen in phenol medium by using a heterogeneous catalyst comprising metals with transient valence. At the second step method involves condensation of oxidation products and non-oxidized products by using a heterogeneous acid catalyst. Separation of compounds in the process of phenol treatment is carried out on the final step of isolation of the commercial product by distillation method. At the first stage metal compounds of by-side subgroups 1 and 6 and metals of 8 group of Periodic system on neutral or acid carrier are used as a catalyst preferably. At the second step alumosilicate contacts based on zeolites of type "X" or "Y", or other zeolites comprising or not comprising promoting and modifying additives are used as a catalyst. Invention provides the high degree of purification of phenol from impurities and the improvement of economy indices of the process.

EFFECT: improved method for phenol treatment.

12 cl, 5 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: industrial organic synthesis.

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

EFFECT: enhanced process efficiency.

3 cl, 1 dwg, 1 tbl

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

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

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

9 cl, 1 ex, 1 dwg, 1 tbl

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

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

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

13 cl, 4 ex

FIELD: chemical technology.

SUBSTANCE: invention relates to a method for purifying phenolic flow prepared after distillation of raw acetone in separating decomposition products of cumene hydroperoxide from hydroxyacetone by rectification method. For removal of hydroxyacetone from phenolic flow methods of azeotropic-extractive rectification is used with using a combined separating agent wherein hydrocarbon (cumene and/or α-methylstyrene) is used as one components, and water is used as another component. Method involves feeding a separating agent in common with feeding a column, maintaining the mass ratio of hydrocarbon and water that equal or above the mass ratio of concentrations of hydrocarbon and water in the corresponding azeotropic mixtures, removing hydroxyacetone from column with distillate aqueous flow and feeding organic phase to phlegm wherein this organic phase is depleted with hydroxyacetone. Use of this method provides enhancing selectivity and complete distillation of hydroxyacetone.

EFFECT: improved purifying method.

17 cl, 2 dwg, 13 ex

FIELD: chemistry.

SUBSTANCE: invention relates to the method of obtaining phenol and acetone by acid-catalysable decomposition of hydro-peroxide of cumene in the environment of the reaction products at elevated temperatures in one stage. In this case the process is carried out in the presence of a catalyst, prepared immediately before its introduction into the reactor for the decomposition of hydro-peroxide of cumene by mixing sulfuric acid with phenol at the ratio of from 2:1 till 1:1000 and the waiting time from mixing till putting into the reactor for the decomposition of hydro-peroxide of cumene from 1 to 600 minutes at a temperature from 20 to 80°C. As a rule, sulfuric acid has a concentration of higher than 75% or oleum is used.

EFFECT: it makes it possible to decrease the output of the by-product hydroxyacetone, improves the quality of market-grade phenol and decreases the consumption of sulfuric acid.

2 cl, 4 tbl, 4 ex

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