CS248562B1 - A method for the complex processing of by-products from the production of phenol and acetone and apparatus for carrying out this process - Google Patents

Abstract

The solution concerns a method of complex processing of by-products from the production of acetone and phenol, so-called phenolic resins, by catalytic decomposition of cumene hydroperoxide into valuable organic oxygen and hydrocarbon intermediates and products. Acetone, phenol are isolated, p-cumylphenol is isolated and synthesized from alpha methylstyrene dimers by arylalkylation of phenol on strongly acidic heterogenic catalysts. Catalytic thermal decomposition of a low-solidifying front fraction containing acetophenone, phenol, alpha methylstyrene and dimethylphenyl carbinol, which is dehydrated to alpha methylstyrene. Phenol is extracted and acetophenone and alpha methylstyrene as essential components are isolated by rectification under reduced pressure. p-cumylphenol and higher molecular weight residue are also isolated. High process selectivity is achieved by optimal reaction conditions using criterion parameters. The process is waste-free, it valorizes all significant components. The device suitably utilizes a combination of apparatuses operating mainly under reduced pressure and allows for multiple reactions to be carried out simultaneously in one apparatus.

Description

248 582

BACKGROUND OF THE INVENTION The present invention relates to a process for the complex treatment of by-products, in particular a distillate residue, the so-called phenol-based phenol-acetone production by catalytic decomposition of cumene hydroperoxide, to valuable organic oxygen and hydrocarbon intermediates and products, as well as the related manufacturing equipment.

It is known to produce phenol, cumene and Λ-methyl styrene by catalytically spraying mouse products after distillation of phenol at 250-350 ° C in the presence of hydrogen on a platinum, nickel, molybdenum or tungsten hydrogenation catalyst (NDR pat · 113 343, 122 179 and 117 869) as well as the current production of phenol and acetone based on the catalytic decomposition of cumene hydroperoxide and dimethylphenylcarbinol (2-phenylprop-2-ol) with acidic catalysts, such as sulfuric acid, to form lead products. Similar, by the decomposition of the so-called phenol mixtures in the presence of the aluminosilicate and the zeolite, useful substitutes such as phenol, cumene, ct are present. -methylstyrene and acetophenone [USSR 583 996 (20.7.1976) and Jap. pat., 5-3087 320 (JH, Jan 7, 1977) J. However, the use of other valuable components is also bent. Similarly, the phenol pitch is also thermocatalytic bonded by other patents (U.S. Pat. No. 2,217,175, 4,339,605 and 4,358,618). 702 345} ČSSR author's certificate 118 409 and 121 796} Britský pat, 1,169,291), the disadvantage of which is the emergence of a variety of difficult to isolate substances.

Also known is the isolation of p-cumylphenol from phenol pitches, by distillation of a film evaporator (Czechoslovak author certificate 195> 54) or from a fraction of so-called funded pitches by an extractive cryostat. However, a significant loss of p-cumylphenol, low conjugation of p- cumylphenol, a relatively high concentration of o-cumylphenol, 248 S62 δο precludes their use of more organic synthesis. CX-methylstyrene dimers are not obtained or technically evaluated and acetophenone of sufficient purity is not obtained. There is also a lack of complex processing of the phenolic strands so that all the components obtained can be a semi-product or a final product.

According to the present invention, there is provided a process for the complex treatment of by-products from the production of phenol and acetone by catalytic decomposition of the hydroperoxide, in particular the distillation residue, the so-called phenolic compounds containing phenol, acetophenone, dimatyl-phenylcarbinol, p-cumylphenol, o-cumylphenol, cK-methylstyrene dimers. cX-methylstyrene, with isolation of acetophenone, cis-methyl-styrene, phenol, as well as with isolation and synthesis of cumylphenols, especially p-cumylphenol, hydrocarbons and higher molecular compounds, by distillation and furthermore acetophenone , dimethylphenylcarbinol and phenol from the acetone isolation are distilled or rectified at a pressure of 0.1 to 15 kPa, where a low boiling fraction consisting mainly of acetophenone, phenol, dimethylphenylcarbinol and optionally OH methylstyrene is separated, and a high boiling fraction consisting mainly of of O (-methylstyrene, p-cumylphenol, o-cumylphenol, 0-methylstyrene dimers) the higher molecular weight compounds and / or the fraction containing 80 to 100% cumylphenols with dimeric dimethylsulfite and a desilting residue, wherein the low boiling fraction is thermally cleaved by the acidic heterogeneous catalyst at 140 to 350 ° C, the selective dehydration of dimethylphenylcarbinol with by conversion to 85 to 100%, the resulting reaction mixture being led to extraction of phenol with water and / or aqueous alkali metal hydroxide or alkali metal hydroxide solution, generally after washing with water to remove acetophenone and oocyte methylstyrene by rectification under reduced pressure pressure and the high-boiling fraction are conducted for distillation and / or rectification under reduced pressure to remove α-methylstyrene dimers and at least a predominant amount of o-cumylphenol present in the feed for distillation and / or rectification, concentrated p-cumylphenol purity of 70-100% and higher-molecular viscous residue, with concentrated p -cumylphenol 248 382 © and, in addition to further refining, in particular rectifying the pressure of 0-10 to 10 kPa to achieve a purity of 90 to 100, and separating the dimeric dimers of α-methylstyrene, which together with the major fraction of α-methylstyrene dimers and o-cumylphenol as a primer, or after removing a portion of this feed, along with the phenol and recirculating fraction of the decomposition step, mainly of the α-methylstyrone dimers and the arylalkylene phenol on the p-cumylphenol on the acidic eterogenic catalysts in the bed and / or sus-retard. 60 DEG-180 DEG C., whereby the crude arylalkylate, optionally after removal of the suspended catalyst and the decylenediarylalkylate, is carried out for rectification, mainly for the separately converted phenol, the dimers of .alpha.-methylstyrene and o-cumylphenol which are recirculated and the commercial .beta.-cumylphenol, and / but fraction containing a total of 80-100% cumylphenols with O- -methylstyrene dimers after the addition of phenol leads to a catalysed aryla1 alkylation of formation of p-cumylphenol, while optionally after oddělenikatalyzátore and odkysleni crude arylalkylátu components from the re-isolated Action Task mixture »

Apparatus for making metal containers, heat exchangers, distillation and rectification columns, reactors, pumps, pumps, separators, condensers, pipes, fittings, measuring sensors, measuring and regulating apparatus, including auxiliary devices, comprising rectifying columns, preferably operating under reduced pressure and combined with a film evaporator, wherein the column head is connected to a pipeline decomposition reactor of dimethylphenylcarbinol, streaming therefrom to a phenol ex-tractor, from which the extract is separated by phenol and washing up to a column from which the stream of OOC is discharged. a methylstyrene and a bottom stream of acstpfenone, a distillation residue is removed from the fifth column together with a recycled stream of z-arylalkyl linker connected to a rectification column connected to a further detection column coupled to a film evaporator for further fractionation of the -O-methyletyrene dimers. cumylphenol, side collection technical cumylphenol, coupled to the final rectification column, where pure p-cumylphenol is removed from its stream. The δ-methylstyrene and o-cumylphenol dimers from the β-24β $ 82 stream are removed from the column by high-boiling higher molecular weight residues, the column head streams are combined and fed to the arylalkylator provided feedstock and fed through the catalyst through two streams to one of which a stream of fresh phenol from the rectification column is provided, with a phenol fraction removed from the column head and a column residue removed from the column. The advantage of the method of complex processing of the distillation residues from the production of phenol, so-called phenolic smfil, according to the invention is the selective isolation and production of component acetophenone, O-methylstyrone, p-cumylphenol, phenol and, as a rule, also dimeric methyl esters of higher molecular weight. phenol smfil residues, then technically-economically evaluating Qfr * methylstyrene dimers, achieving high arylalkylation efficiency of phenol, using reaction bases and suppressing the "acidity" of intermediates, not least the fact that the whole process is desolate. The variability of the content depends on the raw material possibilities and the goal of further technical processing of the individual components, as well as the closure of the whole process. An advantage is also the efficient device, which enables to divide the hard-insulating components of phenol and lead the process of production, obtaining and utilization of components of phenol with minimization of energy consumption and equipment.

SUMMARY OF THE INVENTION The subject of the invention is the treatment of by-products, in particular the distillation residue from the production of phenol and acetone by catalytic decomposition (HgSO4), of a strong acid cation and / or cumene hydroperoxide, the so-called phenolic pitch. Of the hydrocarbons, these are primarily dimers of ofemethylstyrene consisting mainly of: 2,4-diphenyl-4-methyl-1-pentene, trans-2,4-diphenyl-4-methyl-2-pentone, cis-2,4-diphenyl; -4 "methyl» 2-pentene-1,1,1-trimethyl-3-phenylindane. Typically, the latter is about 5% rel., 2,4-diphenyl-4-methyl-1-pentene, about 75% rel., In trans-methylstyrene dimers, and trans-2,4-diphenyl-4-methyl- 2-pentene about 14% rel. The remainder consists of cis-2,4-diphenyl-4-methyl-2-pentene and admixtures of other, more non-detectable hydrocarbon compounds. Oligomers of < RTI ID = 0.0 > methylstyrene < / RTI > Higher molecular weights also include higher condensed, reepiarylalkylated phenols and the like. For some applications, β-cumylphenol may not completely eliminate Q-methylstyrene dimers, as they may fulfill, for example, solvent functions.

The heterogeneous arylalkylation catalysts are mainly phosphorous oxides, phosphates and polyphosphates, but most commonly on carriers / silica, alumina, aluminosilicates and the like, active / bleaching / clay, further synthetic and naturally zeolites, organic cationic / sulfonated copolymers. -merly styrene-divinylbenzene resins, sulfonated polypropylene, sulfonated styrene copolymers, sulfonated phenol-formaldehyde resins, etc., alkaline earth hydrophosphates, zirconium oxide, heteropoly-alkylenes, and the like.

The catalyst is in a bed or suspended in an aryl-alkylation medium. From the crude arylalkylate, in the case of the use of a suspended catalyst, it is necessary to remove it from the environment because it would catalyze the decomposition of p-cumylphenol and other undesired reactions during distillation. as the purpose of removing any catalyst residues or other "acidic" components, neutralizing the arylalkylate with, for example, alkali carbonates, optionally with alkaline earth carbonates, The use of alkali metal hydroxide is generally unsuitable because it would also form Alkyl silicates, alumina with a high specific surface area, or alumina with zirconium oxide are less suitable. cat and cationics, on the one hand, as a result of their low lifetime, but also that they effectively catalyze undesired oligomerization of methylstyrene in this technological step - 7 - 248 S82 (methylstyrene), as well as the fact that contacting is done for the presence of water or water vapor,

Phenol extracoia is carried out either with water or with an alkali metal hydroxide, most often with sodium hydroxide, rarely with potassium hydroxide or calcium hydroxide.

The arylalkylalphenol of the dimer can be performed discontinuously, semi-continuously or continuously. However, semi-continuous laikas have the highest yields. Further steps of the complex treatment may also be continuous, semi-continuous or discontinuous. Further details of the method, as well as devices for complex processing of the primary products, in particular the distillation residue of phenol and acetone production, and other advantages are apparent from the examples.

So-called. phenol pitch from phenol and acetone production by catalytic decomposition of cumene hydroperoxide, consisting (by weight) of 0.2? -methylstyrene, 10.7 acetophenone, 8,4 dimethylphenylcarbinol, 4,4 phenol, 4,9 o-cumylphenol , 26.6 p-cumylphenol, 21.9 dimers-methylstyrene, and 22.5 higher boilers were passed. v. (line 1) (Fig. 1) stream 6 as a feed into the rectification column 2, where the low-boiling components are separated from the prilling particles under reduced pressure (1.3-3.7 kPa). The low boilers, consisting of methylstyrene, acetophenone, phenol and dimethylphenylcarbinol, are passed through a stream (line) of the decomposition of dimethylphenylcarbinol 4 in which at activated alumina (Cherox3 300) at 250 ° C of 20 ° C dehydrates dimethylphenylcarbinol to -methylstyrene (and water). The reaction mixture is passed through a stream (downstream) to an extractor 6, into which an aqueous solution of sodium hydroxide is fed through a stream (line), while the present phenol is reacted with sodium phenolate and withdrawn in the form of an aqueous solution of sodium phenolate. Sallow 8-248,582 processes in the production phenol. Phenol Extract and Pre-wash with Water, consisting essentially of acetophenone and β-methyl-styrene with a stream / line (9) adjacent to the rectification column (10) where a low-pressure head (13 kPa) is blown off the column. / by piping / 11 [alpha] -methyletyrene and from the fifth column by 10 stream / tube / 12 acetophenone,

The distillation residue from the vacuum rectification column 2, any of the dimers of x-methyletyrene, cumylphenols and higher-boiling components, also containing acetophenone admixtures, is co-streamed with 8 recycled stream 31 of arylalkylation in arylalkyl 21 from rectification column 30 , in addition to the cracking column 14 connected to the film evaporator, where the fractionation of the dimers of styrene styrene with o-cumylphenol is separated and removed via a conduit / conduit / 15 to the arylalkylation reactor 21, 91% -1% by weight cumylphenol, and next to the final rectification column 19, where the α-methylstyrene and o-cumylphenol * z pStyl columns are distilled off under reduced pressure (1.33 kPa) and the column 18 is pumped off. with high current / conduit / 17, high-boiling, high-boiling "debris" residues for further use are withdrawn »p-cumylphenol o is discharged from the fifth column 19 with a siphon / conduit / 20 Connected streams 15 and 18, which mainly contain .alpha.-methylstyrene dimers and o-cumylphenol, are obtained after a portion of the solution has been removed by stream / line 27 to prevent the accumulation of o-cumylphenol, such as acetophenone, into the arylalkylator 21. , with the arylalkylation catalyst in the bed or in suspension 1, the stream 26 is fed continuously, discontinuously or semi-continuously, with the dimers of methyl-styrene with the admixtures of o-cumylphenol and acetophenone with a stream 26, whereby an aryl-alkylating stream is fed to the other stream / line (25). catalyst / active bleaching earth / and stream / sink / 28 of rectification column 30 containing regenerated phenol with admixtures of cumylphenols, dimers and optionally primesamacetophenone and o-methylstyrene, to which is added a supply of 33 fresh phenol, from arylalkylation reactor 21 9 - 248 582 in which the arylalkylalphenyl phenol is undergoing dimeric methyl methacrylate, together with the α-methyls tyrene and / or "in situ" of dimers or dimethylphenylcarbinol, the crude aryl-alkylate is continuously, discontinuously or semi-continuously flowed through line (22), added together with the catalyst to separator 23 where it optionally separates the catalyst and is passed through stream 24 and then all or after separation of 15 masses, which is fed by a stream 34 through stream 24 to arylalkylator 21, the crude product of stream 22 or separator 23 ' by stream 29 is fed to a rectification column 30 ' 33 kPa). The unconverted phenol, possibly with the α-methylstyrene, cumenephenols, aethophenone and α, β-methylstyrene, and a mixture of mainly low-reactive α-isomers of β-C-methylstyrene dimer β and, where appropriate, a relatively small reactive isomer is recovered from the thyrous stream 32, o-cumylphenol · The .alpha.-methylatyrene-containing rainwater residue is generally discharged with the stream (13) together with the stream (13) .beta.-cumylphenol together with the dimeric styrene and the higher molecular compounds into the rectification column (14).

The procedure is similar to that of Example 1, but the arylalkyl oxalate 21 is carried out semicontinuously using white clay (active clay) as the ary lactic acid catalyst prepared by activating the bentonite of this composition ($ / wt / wt):

SiO 2? 54.7)? 20? With 18.6 $ MgO = 3.9) CaO = 2.2) Pe?

KgO = 0,2) TiO 2 = 0,2) NagO as 0,1) loss of annealing = 17,4) water StJO) acidity (as HCl) <0,03) bulk density = 500 kg ^ m “' ^ »

To the arylalkylator 21, a regenerated and fresh phenol of an amount of 50.9 wt.% And a bleaching earth were used as catalyst in a quantity of 1 part by weight. Incrementally, 49.1 parts by weight of a fraction of dimers in the methane dimer formed 38.5 wt. parts, o-cumylphenol 10-248,582 8.4, p-cumylphenol> 1.8, n-methylstyrene 0.2 and acetophenone 0.1 wt. a stream 22 to a separator ff liter) 23 &apos;, where the catalyst and the filtrate are separated by a composition (in% by weight) of 24.0 phenola, 10.5 dimers of cZ-methylstyrene, 8,6 o-cumylphenol and 56,1 p- the cobylphenol with the 29-line in the rectification column J0, the cell 20 operating at a pressure of 1.33 kPa and the reflux ratio of 3: 1 ·

At the top of the column, a fraction of phenol is collected in an amount of 23.5 wt. Sausage containing (in% w / w): 98.5 phenol, 0.8 cZ-methyl-styrene and 0.5 oetophene &amp; nu · 75.5 wt. of this composition (in% by weight): 13.8 dimeric β-methylstyrene} 11.3 ovicylphenol} 73.8 β-cumylphenol} 73.8 β-cumylphenol · Example 3 From the so-called phenol smdl, ioh by differential distillation from by X · s with t · 27 to θ6θ ° θ / 2, 67 kPa and II · frakoi of tv · 16O to 210 ° C / 2.67 kPa of this composition (in% by weight): o-cumylphenol = 8 , 4j p-cumylphenol = 50,5} dimers of 4-methylstyrene = 38,3} phenol = ss 0,7} dimethylphenylcarbinol = 0,2} Z-methyl styrene = 0,2} acetofe-non with 0,3 This fraction containing a total of 97.2% of cumyl-phenol dimers is condensed with phosphorus trichloride with stirring at 75 ° C for 2 hours (mole ratio of cumylphenol / phosphorous &amp; 0.25), then further increasing the temperature in two-hour intervals from 100 to 120-150 ° C. The liberated hydrogen chloride is absorbed with an aqueous solution of sodium hydroxide at a concentration of 40% by weight. The remainder of the hydrogen halide is removed by blowing off the air. The obtained phosphated product can be used as a non-benzoic antioxidant, reducing agent and the like. The so-called "phenol smdl" is rectified on the rectilinear column with an efficiency of 25 theoretical degrees, at a reflux ratio of - 11 - 248 582 5 J 1, the fraction ot, v, 110-190 ° 6 / 2.67 lcPae is obtained. by adding phenol to a phenol *: weight fraction of the tv 110-190 ° C / 2, δ7 kPa = 1: 1. The composition of the teat material on arylalkyl is such (in% tomato 4: phenol 51% dimers-methyl styrene = 40.8 $ o-cumylphenol = 8.2 µm-p-cumylphenol £ 0.05). discontinuous arylalkylaleate The discontinuous arylalkylalphenol is carried out in the presence of 2% by weight of clay catalyst, calculated as the arylalkylation mixture, at a temperature of 130 ° C, with vigorous agitation for 2 hours. The product has the following composition (v / w): 7,1 o-cumylphenol $ 39.2 p-cumylphenol 18.9dimers o-methylstyrene and 34.5 phenol Conversion of dimerylstyrene = 53.4% and selectivity of the converted dimers. Tylstyrene to p-cumylphenol = 99.6 The individual components are isolated similar to Example 2. b) The semi-continuous arylalkylae of phenol is carried out such that the phenol / active clay blend (2% by weight of the resulting reaction product) is the fractions are continuously added over a period of 1 h of phenolic mixtures having a boiling point of 110 to 190 ° C / 2.67 kPav by weight equal to phenol (wt. Phenol Ifrakc. 110 to 190 ° C at 2.67 kPa = 1 · i). The composition of the obtained reaction product is as follows (in% by weight): o-cumylphenol (= 7,7) p-cumylphenol = 54,7 $ dimers; 6,

The conversion of the dimeric styrene = 77.4% and the selectivity of the conversion of the dimeric styrene dimer to p-cumylphenol = 96.5%. the fraction of tv, I60 to 210 ° C / 2.67 kPa of this composition (in% by weight): o-cumylphenol = 4,9 $ p-cumylphenol «25,2 $ dimers of methylstyrene = - 18,7 $ ckUthylstyrene e 0.1 $ aetophenone = 0.1 $ dimethylphenicol-binol = 0.1 and phenol 0.3. This fraction is mixed with phenol in a weight ratio of - 12 - 248 582 1: 1 and is continuously poured into a stream of polyphosphate catalyst (or phosphorous oxide (or phosphorous oxide) in a volume of 0 t 3 m 3 / m 3 in the stream. h “l 9 working at 160 ± 3 ° C · The arylalkylate obtained has the following composition (in% by weight): o-cumylphenol = 4,9} p-cumylphenol = 43,8} dimers-methyl malt = 6 , 5} © Ame tyl styrene = 0,05} aceto-phenon = 0,2} dimethylphenylcarbinol with 0,05 and phenol = 43,9.Arylalkylate is divided into 2 parts · The first is subjected to differential distillation without pretreatment · 1 to 30 ° C / 2.67 kPa is obtained in an amount of 45.8% by weight of feedstock with the following composition (<% by weight): o-mole styrene and 3.3% acetophenol. non s 0,3} dimethylcarbinol <<0,05} dimers of--methyl styrene with 3,7a phenol 92,4 · Then II frakio in t> 100 to 210 ° C / 2,67 kPav amount 31,6% of the shaft and of this composition (% by weight): »<f-me-tjftstyrene = 6,3} acetophenone with 0.07% dimers of cis-methyl styrene 18.6} phenol = 15.1% o-cumylphenol = 10.1 and p-cumylphenol = 49.2. Desilatory residue is 22.6% by weight *

The second part of the arylalkylate after the addition of 2% by weight of carbonate-free anhydrous to neutralize the product is distilled off similarly as in the previous case. The fractions are obtained at 30 to 160 ° C / 2.67 kPa in an amount of 45.9% by weight. From a seed shaft and having this composition (% by weight): tf-methylstyrene = 0.6} acetophenone = 0.4} C-methylstyrene dimers = 2.5 afenol 96.0 &lt; tb &gt;

Thereafter, the fractions are in the range of 160-110 ° C / 2.67 kPa in a quantity of 37.5% by weight of the composition composition (in% by weight): t-methyl styrene = 0.3} acetophenone0.05 } dimers of <RTIgt; x-methyl </RTI> styrene = 17.1% o-methylphenol with 13.1 and p-cumylphenol = 68.5 · The distillation residue from the coating is 16.6% by weight. The effect of neutralizing the arylalkylate on the increase in the phenol phenols, especially the loss (decomposition, dearylaikylaemia) effect in distillation or recurrence. Example 6 248 582

The phenolic fraction obtained by the diaphragm at 160 DEG-210 DEG C. (2.67 kPa) with phenol in a weight ratio of 1 l and having the composition (v / v) r-methyl styrene with 0,1} aetophenone and ° C, 1-dimethylphenylcarbinol = 0,2, phenol and 49,9, dimers of? -Methylstyrene = 18,7, o-cumylphenol = 4,9, p-cumylphenol = 25,2, then 1 wt. The active bleaching clay catalyst and the arylalkylalkyl are carried out at 130-2 ° C with stirring for 2 hours. The crude reaction product obtained after filtering off the catalyst has the following composition (in% by weight): oetophenone with 0.2, phenol = 41.4 , dimers of (methylstyrene = 7,3i o-cumylphenol = 5,2 and p-cumylphenol = 45,7 · Conversion of the methylstyrene dimers is 6 l and the selectivity of p-cumylphenol formation from the <X-methyl styrene dimers) 100% · By fractionating at a reduced pressure (2.67 kPa) on a 25-degree column and a 5: 1 reflux ratio a boiling point of 200 to 202 ° C / 2.67 kPa of this composition can be obtained (v $ mass): 98.8 p-cumylphenol, 0.5 o-cumylphenol, 0.6 dimers of α-methylstyrene and 0.1 phenol ·

Claims (4)

SUMMARY OF THE INVENTION 248 582 1 &quot; A complex process for the preparation of by-products of phenol and acetone by catalytic decomposition of cumene hydroperoxide, mainly deetilizing moiety, &quot; phenol &quot; , dimers of methylstyrene, optionally OO-methylstyrene, with the isolation of acetophenone, O-ethyl-styrene, phenol, as well as 8 isolation and synthesis of cumylphenols, mainly p-cumylphenol, hydrocarbons of C18l higher molecular weight compounds, characterized by eteetetilation the remainder and the tall acetophenone, dimethylphenylcarbinol and phenol from the isolation of acetone e and lead to distillation or rectification at a pressure of 0.1 to 15 kPa where a low-boiling fraction is separated off. mainly consisting of acetophenone, phenol, dimethylcarbinol and optionally methyl-styrene, and a high-boiling fraction consisting mainly of O-methylstyrene dimers, p-cumylphenol, o-cumylphenol, O-methylstyrene and higher molecular weight compounds and / or fraction containing 80 to 100% cumylphenols with <X-methyletyrene dimers and deetilizing residue, wherein the low boiling fraction is eatermally and catalytically cleaved at acidic heterogeneous catalyst at a temperature of 140 to 350 ° C, with the selective dehydration of dimethylphenylcarbinol with a conversion of 85 to 100%, wherein the quenched reaction is conducted for extracting phenol with water and / or an aqueous alkali metal hydroxide or alkali metal hydroxide solution, generally after washing with water, leads to the separation of acetophenone and OG-methylstyrene by rectification under reduced pressure and leads to distillation and / or rectification under reduced pressure. separates the α-methylstyrene dimers and asp with a predominant amount of o-cumylphenol present in the feed for distillation and / or rectification, concentrated p-kuraylphenol purity of 70 to 100% and higher molecular weight viscous residue, the concentrated p-cumylphenol optionally leading to further refining, in particular by recrystallization at 0, From 01 to 10 kPa to achieve a purity of 90 to 100%, whereby further O-methylstyrene dimers are separated, which, together with the main fraction of methylstyrene dimer and o-cumylphenol - 15 - 248 562, are injected, or after a portion is removed from the feed , together with 8 phenol and a recirculating fraction of the major dimer decomposition (% -methylstyrene and arylalkylation of phenol to p-ketylphenol on acidic heterogeneous catalysts in and / or suspensions at a temperature of 60 to 180 ° C, while crude arylaics the latter, after separation of the suspended catalyst and de-acidification of the arylalkylate, this is not converted into rectification, in particular for separation. phenol, dimethylethylstyrene dimer and o-cumylphenol, which are recirculated, and commercial cumylphenol, and / or a fraction containing a total of 80-100% cumylphenols with dimeric methylstyrene after the addition of phenol is led to catalysed arylalkylation with the formation of p-cumylphenol, whereupon the components of the reaction mixture are isolated from the reaction mixture, optionally after separation of the catalyst and acidification of the crude arylalkylate. 2 according to claim 1, characterized in that the low-boiling portion is catalytically cleaved on at least one of the acid catalysts selected from the group consisting of alumina, aluminum oxide by the addition of zirconium oxide, aluminosilicates, preferably alumina-activated or acidic zeolite · 3. The process according to claim 1 or 2, wherein the arylalkylation of the phenol by the OC-methylstyrene and / or OC-methylstyrene monomers is carried out in an acid catalyst, preferably a polyphosphate catalyst or a strong acid, stable cationite and / or with suspended acid catalyst, preferably with active bleaching earth, aluminosilicates and strong acid stable cation · 4, apparatus for carrying out the method according to items 1 to 3, consisting of reservoirs, heat exchangers, distillation and distillation columns, reactors, pumps, pumps, separators, condensers, heat exchangers, conduits, fittings, measuring units, measuring and regulating apparatus including an auxiliary device, characterized in that it comprises rectification columns (2), (10), (14), (19), (30), preferably operating under reduced pressure and combined with a film evaporator, wherein the column head 24848 of the column (2) is connected via a conduit (3) to a decomposition reactor of di-ethyl-phenylcarbinol (4), therefrom (5) to a phenol extractor (6), from which the extract is separated by water and washed with water and next to the stream (9) to the column (1), from which the stream of water / 11 / OC-methylstyrene and the fifth stream (12) to acetophenone, from the fifth column / 2 / to the deactivating stream (13) together with the recycle stream (31) / from arylalkylator / 21 / connected to rectification a spin column (30) connected to a rectification column (14), connected by a filter evaporator, and separating the fraction of the Gfr-methylstyrone-8 dimers by o-cumylphenol, by lateral collection of technical cumene phenol (16), attached to the final rectification column (19) whereby the fifth stream (20) and the pure p-cumylphenol are removed by the stream (18) and the dimethylene styrene and p-cumylphenol dimers and the fifth column (14) by the stream (Y7) high-boiling high molecular weight moieties are removed, while 14 / a / 19 / are combined and fed to an arylalkylator (21) provided with a feedstock (26) and supplied with a catalyst (25) and a stream (28) into which the fresh phenol is fed from the rectification a column (30) having a phenol fraction withdrawn from the top of the column by a stream (32) and a residue removed from a fifth stream (31), 1 in FIG.