MXPA00000307A - Process for the removal of organic and/or inorganic acids from splitting products - Google Patents

Abstract

Process for removing (in)organic acids from an aralkyl hydroperoxide decomposition product comprises:(a) extracting the product with an extractant;(b) treating the organic phase with an ion exchanger;(c) distilling the organic phase to obtain an aqueous phase containing organic acids;and (d) treating the aqueous phase with an ion exchanger. An Independent claim is also included for a process for removing (in)organic acids from an aralkyl hydroperoxide decomposition product, comprising:(i) adding an alkaline phenol stream to the decomposition product;(ii) extracting the mixture with an extractant;and (iii) treating the organic phase with an ion exchanger.

Description

PROCEDURE FOR THE ELIMINATION OF ORGANIC AND / OR INORGANIC ACIDS OF THE PHASES OF DISSOCIATION PRODUCTS The present invention relates to a process for the removal of organic and / or inorganic acids from the phases that are formed in the dissociation of aralkyl hydroperoxides. In particular, the present invention relates to a process for the removal of organic and / or inorganic acids from the phases that are formed in the dissociation of cumol hydroperoxide. In many acid-catalyzed processes a not inconsiderable part of the organic and / or inorganic acids used as catalyst remain in the mixtures that are formed. These, if possible, are separated by a phase separation in an aqueous and an organic phase, while inorganic components, such as, for example, water and inorganic acids, are still dissolved in the organic phase. In the processing of these products, the acid that is still present can produce undesired side reactions, such as acid catalyzed alkylation and condensation reactions, which lead to a loss of performance in terms of valuable products. Therefore, in order to avoid this type of unwanted secondary reactions, it is necessary to separate organic and / or inorganic acids as quickly as possible from the organic phase. A process of great industrial relevance is that of the acid catalyzed dissociation of cumol hydroperoxide in phenol and acetone, a process carried out in obtaining these substances starting from cumol, according to the classic Hock procedure. In said process, in the dissociation reaction catalyzed with sulfuric acid of the cumol peroxide (CHP) in phenol and acetone, a mainly organic acid phase is produced, which contains sulfuric acid. To the foregoing, organic acids are usually added, which can be formed as byproducts in the oxidation of cumol or in acid catalyzed dissociation, so that the total acid content is a little higher. In order to avoid acid-catalyzed alkylation and condensation reactions in the cleavage product and to prevent corrosion damage in the apparatuses used, before separation of the dissociation product into its components, for example by distillation, the acids must be removed quickly of the dissociation product. The above is practically practically carried out by immediately neutralizing the dissociation product formed in the acid-catalyzed dissociation of the cumol hydroperoxide, with aqueous solutions of alkali hydroxides and / or phenolates and the subsequent salting out to remove the alkali sulphate which is shape (described in this way in EP 0 032 255, EP 0 085 289, BP 756 408, DE 1 128 859 and DE 25 12 842). However, in spite of neutralization and acid washing, a not inconsiderable amount of alkali sulphate or alkaline carboxylates remains dissolved and / or emulsified in the cleavage product. For this reason, in the subsequent distillation, salt deposits are always formed, which make it necessary to rinse and periodically wash the evaporator. The high content of salts, which remains in the distillation in the sedimentation tank of the distillation column, also complicates the processing of the residue that is formed in the distillation, so it is necessary to separate the salts of the mixture as soon as possible. of dissociation product. From US 4 262 150 and US 4 262 151, it is also known that by the directed neutralization of the cleavage product that is formed in the acid-catalyzed dissociation of cumol peroxide, maintaining a pH of 2 to 6 and with a subsequent salty washing, an improvement of salt separation can be achieved. In US 5 510 543 another possibility to improve the salt separation is described. This is achieved by adding 3 to 5% by weight of cumol to the dissociation product mixture before neutralization.

Neutralization of the dissociation product mixture formed in the acid catalyzed dissociation of the cumol hydroperoxide, as described in US 3 927 124, is also possible using ammonia, methyl amine or triethyl amine. In this process, often the salty washing required after the neutralization is made difficult because there may be considerable problems of phase separation in the same. For this reason, through the patent document DE 963 520 it is also known to remove the sulfuric acid from the dissociation acid product which is formed in the acid-catalyzed dissociation of cumol hydroperoxide by extraction with a weak, non-volatile carboxylic acid. Document DD 91 643 describes the removal of sulfuric acid from the cleavage product that is formed in the acid-catalyzed dissociation of cumol hydroxide by extraction with water. However, in this way, considerable amounts of water (15 to 35% by weight) are required to reduce the content of sulfuric acid in the dissociation product to less than 10 ppm, quantities that must subsequently be processed before they can be taken to the product. drain. The extraction is carried out in an extraction column with 10 mm Raschig rings, at temperatures of 20 to 40 ° C. This process can also be applied to a partially neutralized dissociation product. From CA 697 600, FR 1 302 848 and SU 118 415, it is further known that the removal of sulfuric acid from the cleavage product that is formed in the acid-catalyzed dissociation of cumol hydroperoxide, without extraction, by using exchangers is possible. of anions, regenerating the anion exchanger with an alkaline hydroxide solution. The use of ion exchange resins for the removal of sulfuric acid from the cleavage product, however, due to the low strength of the anion exchange resins against the cleavage product, causes a proportionally short life of the anion exchanger. DE 198 35 306 discloses a process for removing organic and / or inorganic acids from organic phases, which removes organic and / or inorganic acids from them by extraction and subsequent treatment of the organic phase with a ion exchanger. When using this procedure, large quantities of ion exchangers are required, so considerable cost results from the actuation (regeneration, rinsing and exchange) of the ion exchange resin.

For these reasons, the invention is based on the objective of providing a simple and economical process for the removal of organic and / or inorganic acids from the phases of the dissociation product. In particular, the invention is based on the objective of providing a simple procedure for the elimination of organic and / or inorganic acids from the phases that occur in the dissociation of aralkyl hydroperoxides, such as, for example, cumol hydroperoxide, which allows the obtaining of a dissociation product poor in or free of salts, and thus, easier to process. Surprisingly it has been found that the removal of organic and / or inorganic acids from the phases that occur in the dissociation of aralkyl hydroperoxides is considerably improved and it is more economical to perform, by extraction, a subsequent treatment of the organic phase with an ion exchanger, as well as by a distillative treatment of the organic phase and a treatment of a mainly aqueous phase, separated in the distillative treatment of the organic phase and having at least one organic acid, with a second ion exchanger and / or by adding a flow of phenol to the dissociation product phase before extraction. Thus, the object of the present invention is a process for the elimination of organic and / or inorganic acids from the dissociation product phases that are formed in the dissociation of aralkyl hydroperoxides., by extracting the dissociation product phases with at least one extraction agent and a subsequent treatment of the organic part of the phases with an ion exchanger, characterized in that the organic phases treated with an ion exchanger are treated at least once distillatively, in this treatment at least one organic phase, which has at least one organic acid, is separated from the organic phases, and this phase is treated with a second ion exchanger. The present invention also relates to a process for the removal of organic and / or inorganic acids from the dissociation product phases that are formed in the dissociation of aralkyl hydroperoxides, by extracting the dissociation product phases with at least an extraction agent and the subsequent treatment of the organic part of the phases with an ion exchanger, characterized in that before the extraction, at least one flow of alkaline phenol is added to the phase of the dissociation product. With the aid of the process according to the invention, from organic phases containing organic and / or inorganic acids and inorganic components, the inorganic components and the acids can be removed surprisingly well. An advantage over the known processes is that, in the extraction stage, only about a quarter of the amount of extraction agent required in the usual procedures is required, since, unlike these, a total elimination is not required. of acids. If water is used as extraction agent in the extraction stage, a less dilute solution of sulfuric acid is obtained in comparison with the usual procedures, which, thanks to the concentration, can be used in the process. For extraction, so much water is preferably used, that the phase to be extracted is saturated with water and, furthermore, up to 7% by weight, preferably from 2 to 7% by weight, and very especially preferred from 2 to 4% by weight of water, referred to the phase. An important additional effect of this extraction is the wide elimination of all the salts that were formed in the previous stages of the process. The sulfuric acid residue remaining in the organic phase is removed with a slightly basic ion exchanger, commercially available. The use of an ion exchanger has the advantage that in the organic phase, not only the portion of inorganic acids, but also a part of organic acids, in particular formic and / or acetic acid, is very effectively reduced. In a particularly preferred embodiment of the process, in the course of obtaining phenol from cumol, it is possible, for example, to use phenolate bleach for the regeneration of the ion exchanger used. This is produced throughout the process of obtaining phenol, after the process of cumol, by washing phenol from the top product of the cumol column, which contains mainly cumol and a-methylstyrene, with alkaline lye. By using the phenolate bleach for the regeneration of the anion exchanger, the consumption of pure alkali hydroxide, which is usually used for the regeneration of an anion exchanger, can be avoided, and thus, a considerable advantage can be achieved in terms of costs. In addition, the amount of the phenolate in the phenolate bleach becomes less, which must be acidified for the recovery of the phenol, since in the ion exchanger the acid is exchanged for the phenol, and in this way, part of the phenol. Because of the organic phase, before the treatment in the ion exchanger, a large part of the acids is extracted by extraction, the ion exchanger, which is only used for the further purification of the organic phase, is requested less and less. it has a longer life, which has a positive effect on operating costs. Another advantage of the method according to the invention is that the volume of the slightly basic anion exchanger can be kept relatively small, since it is not necessary to eliminate the organic acids of the organic phase without residues. The organic acids, in particular formic and / or acetic acid, are produced in the subsequent processing of the dissociation product phase, in particular in the separation of cumol and a-methylstyrene from the dissociation product phase in a phase containing mainly water. From this phase, the organic acids can be separated relatively easily by treating the phase with a strongly basic anion exchanger. Although this anion exchanger must be regenerated with caustic soda, since the organic acids are removed from an aqueous phase, it can be maintained in relatively small amounts. With these fundamentals, the action (regeneration, rinsing and exchange) of the ion exchanger produces considerably lower technical and financial costs. By adding according to the invention an alkaline phenol stream to the dissociation product phase before the extraction thereof, small concentrations of the acids present in the dissociation product phase are neutralized and can be extracted as salt of the organic phase. The phenol that enters through the flow remains in the organic phase and is recovered in the processing of the dissociation product phase. With this special embodiment of the process according to the invention, on the one hand, the separation of the acids can be improved, and on the other hand, the phenol which is produced in a flow of alkaline phenol in the processing of the product phase of dissociation and that, until now, was processed in a costly manner or had to be discarded, it can be fed back to the processing. The process according to the invention is illustrated below by way of example with the aid of the dissociation of cumol hydroperoxide, which is an intermediate product of the phenol synthesis of Hock, without being limited thereto. In this synthesis, carried out in a known manner, from cumol and oxygen, cumol hydroperoxide is obtained. This, in an acid catalyzed dissociation reaction, dissociates into phenol and acetone. As the catalyst, acid is used, for example, sulfuric acid. The further description, by way of example, of the process according to the invention relates to the embodiment of the cleavage reaction using acid as a catalyst, but without being limited thereto. The acid phase of the dissociation product, which, in addition to the cleavage products and the by-products, can contain the acid used as catalyst as well as organic acids, which are generated as intermediates in the oxidation of aralkyls, such as, for example, cumol, to remove acids, in a first step of the process according to the invention, is taken to an extraction device, preferably an extraction column. The feed of the dissociation product phase to a liquid-liquid extraction column is preferably carried out under the head, especially preferred just above the pit. Above the column pit, preferably just below the head thereof, the extraction column receives an extraction agent. As such, water or a mixture containing mainly water is preferably used. The feed to the extraction column of the extraction agent and the phase to be extracted is controlled in such a way that up to 14% by weight of the extraction agent enters the extraction column, preferably water or a mixture containing mainly water, referred to the dissociation product mixture. Preferably, so much water or mixture containing mainly water is used, that the phase of the dissociation product to be extracted is saturated with water and for the extraction 7% by weight, preferably 2 to 7% by weight and very especially preferred 2 are further employed. to 4% by weight of water, based on the dissociation product phase. The extraction agent and the phase to be extracted pass through the extraction column in a parallel or countercurrent flow, preferably countercurrent. In a particularly preferred embodiment of the process according to the invention, to the dissociation product phase obtained in the dissociation of cumol hydroperoxide, before feeding to the extraction device, a mixture having phenol is added, which is It produces in the processing of phenol and contains all the caustic soda that was added to the process during the distillative processing of the phenol. During the extraction, from the acid anions present in the cleavage product, with the sodium ions of the phenol-containing mixture, salts are formed which, after extraction, are mainly found in the aqueous phase. In this way it is possible with the extraction not only to reduce the concentration of acid in the organic phase of the dissociation product, but also to reduce the concentrations of salts, such as, for example, Na 2 SO 4. Depending on the initial concentration of salt, or, acid in the dissociation product mixture and the NaOH concentration and the amount of the added mixture having phenol, Na 2 SO 4 concentrations of 1 to 2 ppm can be achieved in the organic phase of dissociation product. According to the invention, the extraction agent, preferably water, charged with acid is extracted from an extraction device, preferably from the lower part of an extraction column. In the case of sulfuric acid as a catalyst, dilute sulfuric acid is extracted from the lower part of the extraction column, which can still be used in the process. The temperature in the extraction device is between 0 and 90 ° C, preferably between 20 and 50 ° C and especially preferred between 30 and 40 ° C. According to the invention, the part of the organic phase of dissociation product, rich in water-soluble ions, obtained from the extraction device, preferably from the head of an extraction column, and which also contains organic acids as well as small amounts of inorganic acids, it is possible to pass through at least one commercially available anion exchanger, preferably slightly basic, such as, for example, Amberlyst A21 or IRA 96 SB from the company Rohm und Haas. The loading speed of the anion exchanger depends on the dimensions of the exchange bed, which, in turn, depends on the volume flows to be treated and their acid concentrations, and can be adjusted by valves or similar devices. In another preferred embodiment of the process according to the invention, the part of the organic phase of dissociation product obtained from the extraction device, rich in water-soluble ions, before treatment with an anion exchanger, to remove the emulsified water is You can first pass through a coalescent. With this, the water level of the organic phase of the dissociation product and the salt loading can be reduced. The aqueous phase separated with the coalescent can be fed to a processing. If the water must be removed, the organic components that are present should be separated, such as acetone and / or phenol. After passing through the extraction device and the anion exchanger, the organic phase of the cleavage product is to such an extent free of inorganic acids that analytically no longer can be detected inorganic acids, and can be processed, preferably Distillation processing The salt content of the organic phase of the dissociation product, after passage through the extraction device using possibly a coalescent and / or anion exchanger, was considerably reduced and is preferably from 1 to 2 ppm, calculated as sulphate of sodium. In the distillative processing of the organic phase of the dissociation product, which can be carried out in a manner known in general, in various stages of distillation of the product itself in the dissociation of cumol hydroperoxide, of the phenol, more and less elevated boiling compounds are separated. In the course of these distillative stages, mainly aqueous phases are also produced, which may have organic acids, such as for example, formic or acetic acid. In addition to these acids, the mainly aqueous phases can also have small amounts of organic products or by-products of the dissociation of aralkyl hydroperoxide, such as, for example, phenol or cumol. It may be advantageous to feed these phases back to the distillation process, to enrich some components, such as, for example, organic acids. These acids reoccur in the mainly aqueous phases. In the same way it can be advantageous to direct these aqueous phases that are produced to a container, in which the organic components can be separated from the mainly aqueous phase. The aqueous phases that are produced, which have organic acids, such as for example formic and / or acetic acid, which may still contain products or by-products of the dissociation of aralkyl hydroperoxide, such as for example phenol, can be used for extraction of sulfuric acid from the dissociation product mixture. In a special embodiment of the process according to the invention, the aqueous phases that are produced, which have organic acids, such as for example formic and / or acetic acid, which may still contain products or by-products of the hydroperoxide dissociation of Aralkyl, such as, for example, phenol, can be prepared with a second anion exchanger, preferably strongly basic. As an anion exchanger, any usual anion exchanger can be used in the market, preferably a strongly basic exchanger, such as, for example, .Amberjet 4400 OH from the company Rohm und Haas. In principle (independently of the example), in addition to the extraction columns, any extraction device that works continuously or discontinuously may be used. Preferably extraction columns equipped with suitable inserts are used. As a slightly basic anion exchanger, commercially available anion exchangers, for example polyacrylamide or styrene-dimethylbenzene reams, such as Amberlyst A 21 or IRA 96 SB from Rohm und Haas can be used. As a strongly basic anion exchanger, commercially available heat exchangers, such as .Amberlyst 4400 OH from the company Rohm und Haas, can be used. The regeneration according to the invention of the anion exchanger can be carried out with bleach, for example, with an alkaline hydroxide solution. For purposes of regeneration, the regeneration solution is passed through the anion exchanger in the same direction or in the opposite direction to the direction in which the phase to be treated flows through the anion exchanger, preferably in the same direction. In a particularly preferred embodiment of the process according to the invention, for the regeneration of the slightly basic anion exchanger a phenolate bleach solution containing free phenol is used, which is produced in the processing of the phenol-containing phases. After regeneration, the anion exchangers can be rinsed with water. The rinsing is preferably carried out until no OH-ion or any alkali or sodium phenolate can be detected in the rinse water, depending on whether the anion-exchange reactant was regenerated with alkali hydroxide solution, for example, with NaOH, or with phenolate bleach, in the anion exchange process, the acids contained in the organic phase result in water or phenol, according to the formulas: Ion exchange process Resin-OH + HX -> Resin-X + H20 Regeneration Resin-X + NaOH -> Resma-OH + NaX Ion exchange process resin phenol + HX- > X-Resin + phenol Regeneration X-Resin + Na phenolate - > Resin phenolate + NaX (X indicates an inorganic or organic acid radical, such as HS04 ~, formate or acetate) If water is produced in the ion exchange process, it can be separated from the organic phase, for example by means of a phase separator . If, in the ion exchange process of the especially preferred process, phenol is produced, it can be fed directly to the processing with the organic phase of the dissociation product. In order to continuously carry out the process according to the invention, it can be advantageous to use at least two slightly basic exchangers and two strongly basic exchangers respectively. These are preferably arranged in such a way that during loading of an anion exchanger the other can be regenerated as described above, and vice versa. The exchange of the exchangers of regeneration anions to ion exchange and vice versa can be carried out with the help of valves, isolation keys or the like, in a manner known to the person skilled in the art. According to the invention, the use of several extraction columns or several ion exchangers or the use of several combinations of extraction columns with subsequent ion exchangers can be envisaged. The extraction according to the invention is preferably carried out at ambient pressure and at temperatures between 0 and 90 ° C, preferably at temperatures between 20 and 50 ° C and especially preferred at temperatures between 30 and 40 ° C. According to the invention, acidic or neutral water, preferably neutral water, can be used as extraction agent. Preferably, the aqueous phase which comes from the container after the distillative processing of the dissociation product phase and which, with the help of the strongly basic ion exchanger, was largely freed from the organic acids and / is used as the extraction agent. or inorganic The process according to the invention can be carried out continuously or discontinuously. It may be advantageous to combine preferred embodiments of the process according to the invention. The process according to the invention is suitable for removing organic and / or inorganic acids from phases that occur in the dissociation of aralkyl hydroperoxides. The process according to the invention is especially suitable for removing organic and / or inorganic acids from phases that are produced in the dissociation of cumol hydroperoxides. In FIG. 1, an embodiment of the method according to the invention is shown by way of example, without limiting the method.

The dissociation product to be treated arrives via line a to the extraction device E. Via line b, a flow of phenol can be introduced into the dissociation product before passing to the extraction device. The organic phase leaves the extraction device via the line c and passes through the anion exchanger Al. In this line, a coalescent K can be provided for the separation of the water emulsified in the organic phase. The aqueous phase that is produced in the extraction device, as well as, if it exists, the aqueous phase that is produced in the coalescent, is collected through the p and q lines, respectively. The phase treated in the ion exchanger Al is carried by line d to a distillation unit D, which consists of several distillation columns. In said unit the processing of the dissociation product is carried out. In this, a mainly aqueous phase is produced, which is carried to the anion exchanger A2 through line f. The organic phases are brought to further processing, for example, through line e. The phase treated in the anion exchanger A2 leaves it through the line j and through it reaches the extraction device E and enters it. Via line g, the anion exchanger A2 can be regenerated with bleach. Through line s, the Al anion exchanger can be regenerated with bleach. The regeneration liquor leaves the anion exchanger A2 through the line k, and the anion exchanger Al, through the line m. Both lines are joined on line 1, through which the regeneration liquor is brought to a dephenolization. Through the lines h and t, rinse water can be supplied to the Al and A2 anion exchangers. Said rinsing water leaves the anion exchangers Al and A2 through the lines i and n, which join in the line o. With this line is also attached the line q, which carries the collected aqueous phases, produced in the extraction device E and / or in the coalescent K. The line or carries these exhaust waters, which may contain phenol and / or acetone, to a desfenolización.

Example 1: Removal of sulfuric acid and organic acids from the mixtures produced in the dissociation of a phase of cumol hydroperoxide In the preparation of phenol and acetone starting from cumol, according to the classic Hock process, in the dissociation reaction of hydroperoxide of cumol, catalyzed with sulfuric acid, to obtain phenol and acetone, an acid phase of the dissociation product is produced, which, in the example presented, contains approx. 950 ppm sulfuric acid. To this organic acids are added, so that the total acid content (calculated as sulfuric acid) is on average of approx. 1200 ppm. The dissociation product phase was passed on an average of 250 1 / h through an extraction column. In addition to the dissociation product phase saturated with water, 4% by weight of water was passed through the extraction equipment. After extraction at a temperature of on average 30 ° C, the content of sulfuric acid in the organic phase was < 20 ppm. The total acid content in the organic phase after this treatment was on average 250 ppm (calculated as sulfuric acid), since organic acids were hardly allowed to be extracted. This organic phase was passed at 225 1 / h through an anion exchange bed, which was filled with 15.3 1 of the slightly basic anion exchange resin, commercially available, .Amberlyst A 21 from the company Rohm und Haas. The temperature of the organic phase was approx. 30 ° C. After passing through the anion exchanger, the treated organic phase was analyzed and it was possible to detect therein a total acid concentration of < 250 ppm, calculated as H2S04. The contribution of the sulfuric acid to the total acid concentration was < 1 ppm.

Example 2: Removal of sulfuric acid and organic acids from the mixtures that occur in the dissociation of a cumol hydroperoxide phase. A phase of dissociation product is passed as in Example 1 by an extraction column., with the difference that with the phase of the dissociation product an alkaline phenol stream was mixed with an average of 8 1 / h. After extraction at a temperature of approx. 30 ° C, the content of sulfuric acid in the organic phase was 100 to 170 ppm. The total acid content in the organic phase after this treatment was still on average 300-400 ppm (calculated as sulfuric acid), since organic acids were hardly allowed to be extracted.

Example 3: An organic phase of the dissociation product treated as in Example 1 was processed in several distillation stages. In this distillative processing an aqueous phase was obtained, which contained the organic acids, in particular acetic and formic acid. The aqueous phase was passed at 225 1 / h through an ion exchange tower filled with 15.3 1 of a strongly basic anion exchange resin (Amberjet 4400 OH, from the company Rohm und Haas). After treatment with the ion exchanger, the acid content was reduced by on average 1000-1500 ppm a on average < 25 ppm, calculated as acetic acid.

Claims (18)

1. A process for removing organic and / or inorganic acids from the dissociation product phases that are formed in the dissociation of aralkyl hydroperoxides, by extracting the dissociation product phases with at least one extraction agent and a subsequent one treatment of the organic part of the phases with an ion exchanger, characterized in that the organic phases treated with an ion exchanger are treated at least once in a distillative manner, in this treatment organic phases are separated from at least one mainly organic phase , which has at least one organic acid, and this phase is treated with a second ion exchanger.

2. A process according to claim 2, characterized in that the organic phase treated with an ion exchanger is distilled at least once in a distillation column.

3. A process according to any of claims 1 or 2, characterized in that a mainly aqueous phase, which has at least one organic acid, which, by the distillative treatment of the organic phase carried out at least once, is separated from it is treated with a strongly basic anion exchanger.

4. A process according to at least one of claims 1 to 3, characterized in that the mainly aqueous phase is used as extraction agent, which was treated with the strongly basic anion exchanger.

5. A process according to at least one of claims 1 to 4, characterized in that before the extraction, at least one flow of alkaline phenol is added to the dissociation product phase.

6. A process for removing organic and / or inorganic acids from the dissociation product phases that are formed in the dissociation of aralkyl hydroperoxides, by extracting the dissociation product phases with at least one extractant and the subsequent treatment of the organic part of the phases with an ion exchanger, characterized in that before the extraction, at least one flow of alkaline phenol is added to the dissociation product phase.

7. A process according to at least one of claims 1 to 5 or according to claim 6, characterized in that up to 14% by weight of water, based on the dissociation product phase, is used for the extraction.

8. A process according to at least one of claims 1 to 5 or according to at least one of claims 6 or 7, characterized in that for the extraction of a dissociation product phase saturated with water, it is further used up to 7% by weight of water, based on the phase of the dissociation product.

9. A process according to claim 8, characterized in that for the extraction of a dissociation product phase saturated with water, 2 to 7% by weight of water, based on the dissociation product phase, is additionally used.

10. A process according to claim 9, characterized in that for the extraction of a dissociation product phase saturated with water, 2 to 4% by weight of water, based on the dissociation product phase, is additionally used.

11. A method according to at least one of claims 1 to 5 or according to at least one of claims 6 to 10, characterized in that the temperature in the extraction is between 10 and 90 ° C.

12. A method according to claim 11, characterized in that the temperature in the extraction is between 20 and 50 ° C.

13. A method according to claim 12, characterized in that the temperature in the extraction is between 30 and 40 ° C.

14. A method according to at least one of claims 1 to 5 or according to at least one of claims 6 to 13, characterized in that the organic part of the dissociation product phases, obtained after the extraction, is treated with a slightly basic anion exchanger.

15. A process according to at least one of claims 1 to 5 or according to at least one of claims 6 to 14, characterized in that the organic part of the dissociation product phases, obtained after the extraction, before of the treatment with a slightly basic anion exchanger, it is treated with a coalescent.

16. A process according to at least one of claims 1 to 5 or according to at least one of claims 6 to 15, characterized in that an alkaline hydroxide solution is used for the regeneration of the anion exchanger.

17. A process according to at least one of claims 1 to 5 or according to at least one of claims 6 to 16, characterized in that phenolate bleach is used for the regeneration of the slightly basic ion exchanger.

18. A process according to at least one of claims 1 to 5 or according to at least one of claims 6 to 17, characterized in that the dissociation product phases that are formed in the dissociation of cumol hydroperoxide are used. .