JPS6350335B2 - - Google Patents

Description

[Detailed description of the invention]

The present invention produces 2,2-bis(4-hydroxyphenyl)propane (hereinafter referred to as p,
It is abbreviated as p′-BPA. ), the p,
The object of the present invention is to provide a method that can prevent the deposition of p'-BPA/PhOH crystals and, as a result, produce high-quality p,p'-BPA/PhOH. p,p'-BPA has been conventionally used as a raw material for polycarbonate and epoxy resins. As the uses and demand for these resins expand, high-quality resins are required, and as a result, p,p'-BPA, which is the raw material for these resins, has a high purity and good color. There is a growing demand for quality products. In particular, p,p'-BPA, which is a raw material for polycarbonate, is required to be of high quality, for example, high quality p,p'-BPA with a purity of 99.9% or more and a melt color of 30 APHA or less. Moreover, it is of course required to produce such high quality p,p'-BPA rationally and economically. In order to economically produce p,p'-BPA that meets these requirements, it is necessary to react the raw materials phenol and acetone at a high conversion rate in one contact, and to selectively p,p′-BPA
It is necessary to produce p,p'-BPA, and it is necessary that the produced p,p'-BPA can be purified by an easy method.
There is also a need for BPA to be of high quality, high yield, and low cost. By the way, when reacting phenol and acetone, the rate of change is low, for example, the rate of change of acetone is 55%.
or when the molar ratio of phenol to acetone is high, the generated p,
p'-BPA is completely dissolved in the reaction mixture, and the reaction mixture excluding the catalyst system in the reaction system is a homogeneous phase. However, even if the reaction is carried out at such a low rate of change, p,p'-BPA cannot be produced economically and the above requirements cannot be met. In order to improve this drawback, if the reaction is carried out by using an excess of phenol relative to acetone to increase the conversion rate of acetone, p,p'-BPA becomes p,p'-BPA.
It crystallizes as PhOH crystals, and the reaction mixture begins to form a slurry mixture. Due to the condensation of catalyst vapor on the vessel wall and the consequent condensation reaction on the vessel wall, or other reasons, the catalyst becomes adhered in a hard layer to the inner wall, stirring rod, etc. above the liquid phase surface in the reactor. This phenomenon of wall adhesion becomes more noticeable as the reaction time progresses when the reaction is carried out in a continuous manner. If this phenomenon of wall adhesion becomes severe, it may become impossible to operate the reactor, or the adhesion may peel off in large chunks, clogging the lines within the reaction system, allowing continuous reactions to continue for a long time. be unable to do so. As a result, in addition to the need for troublesome operations such as periodically interrupting the reaction and removing deposits inside the reactor, when this wall deposition becomes severe, colored by-products accumulate, Heating the reactor to remove this deposit, or opening it to mechanically remove the deposit, introduces air (oxygen) into the reaction mixture, which further increases the formation of colored by-products. So, p like this,
High quality p, p′-BPA from p′-BPA/PhOH
The disadvantage is that it becomes difficult to obtain. When the above reaction is carried out in a continuous manner using hydrochloric acid or hydrogen chloride as an acidic catalyst, the reaction occurs due to the catalytic action of hydrogen chloride vaporized above the liquid phase surface in the reactor, so the above-mentioned This trend will become even greater. Conventionally, p,p'-BPA was produced by reacting phenol and acetone in the presence of an acidic catalyst.
Many methods have been proposed and are known as methods for producing PhOH. For example, a method of using hydrochloric acid or hydrogen chloride as a catalyst when reacting phenol and acetone, and a method of purifying and separating p,p'-BPA from the reaction mixture after the reaction is disclosed in Japanese Patent Publication No. 27-5367. Publication No., Special Publication No. 1973-
Publication No. 23335, Special Publication No. 38-4875, Special Publication No. 1977
-7186 Publication, Special Publication No. 6333, Special Publication No. 1973
−3379 Publication, Special Publication No. 47-10384, Special Publication No. 10384, Special Publication No. 10384
50-128428, JP 48-97853, JP 49-93347, JP 49-82651,
It has been proposed in JP-A-53-101347, JP-A-54-98748, JP-A-54-98749, and others. None of these prior art documents provide any prescription for improving the aforementioned problems caused by wall adhesion of p,p'-BPA/PhOH. The present invention has been made in view of the above-mentioned problems existing in the technical field of manufacturing p,p'-BPA/PhOH and the current state of the prior art in this field, and its purpose is to In a method for producing a slurry reaction mixture containing crystals of p,p'-BPA/PhOH by reacting phenol and acetone in the presence of an acidic catalyst,
p, p′-BPA・ on the inner wall above the liquid phase surface of the reactor.
By suppressing the phenomenon of PhOH crystals and other solids adhering, the reaction rate is accelerated and long-term continuous reaction is possible, while high quality with low content of high-boiling and colored by-products. The object of the present invention is to provide a method for economically producing p,p'-BPA.PhOH. More specifically, by performing the reaction while injecting the raw material supplied to the reactor into the inner wall of the reactor from a nozzle provided above the liquid phase surface of the reactor,
This is based on the discovery that the above object can be achieved. Briefly, the invention consists of reacting phenol and acetone in the presence of a soluble acidic catalyst to form a slurry reaction mixture containing crystals of p,p'-BPA PhOH. In the method for producing p,p'-BPA.PhOH, the reaction is carried out while injecting at least a part of the raw materials supplied to the reactor onto the inner wall of the reactor from a nozzle provided above the liquid level of the reactor. This is a method for producing p,p'-BPA/PhOH, which is characterized by the following. In the method of the present invention, phenol and acetone are reacted in the presence of a soluble acidic catalyst, and in the reaction system the reaction mixture forms a slurry reaction mixture containing crystals of p,p'-BPA.PhOH. In the method of the present invention, the soluble acidic catalyst, reaction conditions, and reaction method used for the condensation reaction of phenol and acetone are such that the reaction mixture generated in the reaction system contains crystals of p,p'-BPA.PhOH. There are no particular limitations as long as a slurry reaction mixture is formed. These will be described later. In addition to p,p′-BPA・PhOH produced in the condensation reaction of the present invention, 2-
(2-hydroxyphenyl)-2-(4-hydroxyphenyl)propane (hereinafter abbreviated as o,p'-BPA), 2,2-bis(2-hydroxyphenyl)propane (hereinafter o,p'-BPA), o'-BPA); 4-(4-hydroxyphenyl)-2,2,4-trimethylchroman (hereinafter abbreviated as codimer); 2,4-bis (α,α-dimethyl-4-hydroxybenzyl)
Phenol (hereinafter abbreviated as BPX), 2-(2
-hydroxyphenyl)-2,4,4-trimethylchroman (hereinafter abbreviated as o-dimer), 5
-Hydroxy-3-(4-hydroxyphenyl)-
1,1,3-trimethylindan (hereinafter referred to as IPEP)
high boiling point by-products such as cyclic dimer), 2,4-bis(4-hydroxyphenyl)-4-methyl-1-pentene (hereinafter abbreviated as IPEP linear dimer); By-products such as colored by-products of unknown structure are generated. Most of the target product p,p'-BPA forms phenolic adducts. In the method of the present invention, the slurry reaction mixture formed by the condensation reaction is a slurry reaction mixture containing p,p'-BPA.PhOH crystals as a main component as a suspended solid component. The slurry reaction mixture contains p,p′-BPA・
In addition to PhOH crystals, the above-mentioned byproducts may also be included. In addition, the mother liquor component constituting this slurry reaction mixture is p,p'-BPA or p,p'-
It may be a homogeneous phase mother liquor containing BPA/PhOH, unreacted phenol, unreacted acetone, the above-mentioned by-products, produced water, acidic catalyst, etc., or p,p'-BPA
or p,p′-BPA・PhOH, unreacted phenol,
Unreacted acetone, an oil phase mother liquor consisting of the above-mentioned by-products, an acidic catalyst aqueous solution, unreacted phenol, unreacted acetone, and a trace amount of p, p'-BPA or p, p'-
In some cases, it is a two-liquid phase mother liquor consisting of both an aqueous phase mother liquor consisting of BPA, PhOH, etc. In order to increase the conversion rate of acetone and to increase the selectivity to p, p'-BPA and its yield, it is necessary that the mother liquor components constituting the slurry reaction mixture form the two-liquid phase mother liquor. is preferable, and the weight ratio of the aqueous phase mother liquor to the oil phase mother liquor is usually in the range of 0.01 to 2, preferably 0.03 to 1.2. In the method of the present invention, the reaction is carried out while injecting at least a portion of the raw material supplied to the reactor onto the inner wall of the reactor from a nozzle provided above the liquid phase surface of the reactor. As a result, the contact state of the raw materials is improved, and the reaction rate is also improved. Examples of raw materials supplied to the reactor include raw material acetone, raw material phenol, acidic catalyst, and mother liquor for circulation described below. The ratio of the raw material that is injected onto the inner wall of the reactor from the nozzle provided above the liquid phase surface in the method of the present invention to the total raw material supplied to these reactors is not particularly limited, but is usually 0.2 to 0.2. 1. Preferably
It ranges from 0.4 to 1. As the injection supply method, a method is employed in which the material is injected onto the inner wall surface of the reactor from a nozzle provided at an arbitrary position above the liquid phase surface in the reactor. At this time, it is preferable to supply the injection feedstock so that it is spread over the entire inner wall surface of the reactor. For this purpose, the tip of the supply nozzle must be provided with a plurality of injection ports so as to be able to spray in all directions, or the tip should have at least one injection port that can be provided so as to be able to spray toward the inner wall surface and be able to rotate. This is achieved by installing a nozzle. As the latter method of spraying and supplying using a rotating nozzle,
It is also possible to adopt a method of supplying the raw material to a hollow stirring shaft of a rotary stirrer, injecting it from a supply nozzle provided at any position on the liquid phase surface of the hollow stirring shaft or stirring blade, and feeding it while rotating. can. Furthermore, the injection supply may be carried out in any condition as long as the cleaning effect on the inner wall surface of the reactor can be sufficiently exerted, and the supply condition is not particularly limited. For example, various methods such as a method of supplying in a spray state and a method of supplying in a jet state can be adopted. In the method of the present invention, phenol and acetone are usually reacted by the following method. Examples of the soluble acidic catalyst used in the reaction include ordinary strong acidic protonic acids, preferably strong acidic inorganic acids. Specifically, strong acidic inorganic acids include hydrogen fluoride, hydrofluoric acid, hydrogen chloride, hydrochloric acid, hydrogen bromide,
Examples include hydrogen halides or hydrohalic acids such as hydrobromic acid, sulfuric acid, and nitric acid. Among these strongly acidic protic acids, it is particularly preferable to use hydrogen chloride or hydrochloric acid, and in particular, using a hydrochloric acid-containing catalyst, the reaction mother liquor of the slurry reaction mixture can be converted into an oil phase mother liquor and an aqueous phase mother liquor as described above. It is preferable that a two-liquid phase mother liquor is formed. The proportion of the soluble catalyst used is usually 0.5 to 5 moles, preferably 1 to 5 moles, based on the protonic acid contained in 1000 g of the slurry reaction mixture. In the method of the present invention, the soluble acidic catalyst alone can be used as the acidic catalyst, but a soluble acidic catalyst and other promoter components can also be used in combination. Conventionally known cocatalysts and components are used, and usually a sulfur-containing compound soluble in the reaction mixture is used, either a gaseous sulfur compound, a liquid sulfur compound, or a solid sulfur compound. can do. Specifically, these promoters include inorganic sulfur compounds such as sulfur monochloride, sulfur dichloride, sodium thiosulfate, potassium thiosulfate, and hydrogen sulfide; alkyl mercaptans such as methyl mercaptan, n-propyl mercaptan, and n-butyl mercaptan. Thiophenols such as thiophenol, p-methylthiophenol, p-ethylthiophenol, p-chlorothiophenol, thiohydroquinone, and thionaphthol; Mercapto-substituted fatty acid carboxylic acids such as thioglycolic acid, thioacetic acid, and thiopropionic acid ; the alkali metal salts of the alkyl mercaptans, the thiophenols, and the mercapto-substituted aliphatic carboxylic acids;
Examples include mercaptals and mercaptols derived from the mercaptans. When these sulfur compounds are used as cocatalysts, the molar ratio to the soluble acidic catalyst in the reaction system is usually 1/2000 to 1/2000.
30, preferably in the range of 1/1000 to 1/50. The molar ratio of total phenol to total acetone supplied to the reactor during the reaction is usually 4 to 20,
Preferably it is in the range of 5 to 10. It is preferable that the molar ratio of total phenol to total acetone is within this range, since a slurry reaction mixture with good properties will be formed. Further, during the reaction, the reaction is carried out until the rate of change of acetone usually reaches 90% or more, preferably 95% or more. The greater the rate of change of acetone during the reaction, the better the properties of the slurry reaction mixture can be obtained. The temperature during the reaction is usually in the range of 25 to 70°C, preferably 30 to 60°C. In the process of the invention, unreacted phenol and unreacted acetone separated from the slurry reaction mixture can also be fed as part of the feedstock of the process of the invention. Further, all or part of the reaction mother liquor separated from the slurry reaction mixture and containing the acidic catalyst and the by-products may be supplied to the reaction system as the raw material. Next, an outline of an example of a process diagram for carrying out the method of the present invention will be explained with reference to FIG. FIG. 1 is an example of a system diagram of a continuous condensation reactor for carrying out the method of the present invention. The supplementary raw material tanks 1 and 2, the circulating oil phase mother liquor tank 3, and the circulating water phase mother liquor tank 4 are the first reaction tank 11 and the second reaction tank 1 in the reaction process.
This is a device for continuously supplying raw materials to a serial multi-stage reactor consisting of a second and a third reaction tank 13, in which a continuous condensation reaction of a reaction step is carried out, and a slurry reaction mixture is produced. is formed and the slurry reaction mixture is collected in receiver 14. The slurry reaction mixture is separated into crude p, p'-BPA/PhOH and a two-liquid phase reaction mother liquor in the centrifugal separator 15 in the next separation step, and the two-liquid phase reaction mother liquor is further separated into oil and water in the next circulation step. The liquid is separated into an oil phase mother liquid and an aqueous phase mother liquid in a vessel 16. After a portion of the separated oil phase mother liquor and aqueous phase mother liquor are discharged from 17 and 18, respectively, as necessary, the remaining mother liquors are recycled to the reactor for the reaction step. During circulation of aqueous phase mother liquor, HCl absorption tank 5
After being saturated or supersaturated with the supplied HCl gas 6, it is circulated. Next, the method of the present invention will be specifically explained using examples. In addition, in Examples and Comparative Examples, the rate of change of acetone, the reaction mixture in the reaction system
The amount of soluble acidic catalyst contained in 1000 g of each sample was measured by the following method. Also, rough p, p′−
BPA/PhOH circulating oil phase mother liquor, p, p'-BPA, phenol, water, HCl contained in circulating water phase mother liquor,
The composition of the by-products was determined by each method. 1. Method for quantifying unreacted acetone The acetone conversion rate was determined by dissolving the reaction mixture in an ethanol solvent, neutralizing it, and quantifying unreacted acetone using gas chromatography. 2. Determination of phenol and p,p'-BPA Phenol and p,p'-BPA were determined using gas chromatography. 3 HCl quantitative method After dissolving the sample in ethanol solvent, HCl is
It was quantified according to the usual neutralization titration method. 4 Method for quantifying by-products By-products were quantified using high-performance liquid chromatography after dissolving a sample in ethanol and neutralizing it. 5 Measurement of coloration degree of circulating oil phase mother liquor and crude p,p'-BPA/PhOH Place the sample in a volumetric flask, dilute with ethanol, fill a 10 cm cylindrical glass cell with this diluted solution, and use a Spectronic 70 spectrophotometer. [Baush &L'ombe]
Absorbance (or transmittance) at 360 nm and 480 nm was measured using a 360 nm and 480 nm probe manufactured by Romb Co., Ltd. The concentration of the sample used in the measurement was changed as appropriate depending on the degree of coloration of the sample. The degree of coloration of the sample was expressed using the following formula. E1% 1cm=A/cb...(1) ^* Here, A=absorbance, c=sample concentration (W/V%), b=cell length (light path length) (cm) The following implementation Indicated in examples and comparative examples
E480 indicates E1% 1 cm at a measurement wavelength of 480 nm. In addition, Figures 2 and 3 show the reaction time (hr) of the circulating oil phase mother liquor and crude p,p'-BPA/PhOH.
(horizontal axis) and degree of coloration at 480nm (E1% 1cm×
10 ⁴ ) (vertical axis) is shown in a graph. (*) Robert, M. Silverstein, G. Glaytom Bassler, translated by Shun Araki and Yoichiro Mashiko (Tokyo Kagaku Dojin), “Spectral identification of organic compounds. Method 6: Measurement of weight ratio of aqueous phase mother liquor to oil phase mother liquor in slurry reaction mixture The slurry reaction mixture flowing out from the reaction tank is received in a storage tank kept at the same temperature as the reaction tank. Once a certain amount of the reaction mixture had accumulated in the storage tank, it was placed in a centrifuge kept at the same temperature as the reaction tank and rotated until the cake was almost dry. The mother liquor discharged from the centrifugal separator was led to a static tank, and oil and water were separated. Next, the volume and specific gravity of each phase were measured, and the weight ratio of the aqueous phase mother liquor to the oil phase mother liquor was determined. 7 Quality Assay Method for Purified p,p'-BPA (1) Freezing Point A sample and an immersion line thermometer (ASTM102) were placed in a measuring tube, cooled in a thermostat at 140°C, and measured according to the usual method. (2) Analysis of organic impurities Analysis was performed using the same high performance liquid chromatography as in 4 above. (3) Measurement of coloration degree E ₃₆₀ and E ₄₆₀ Dilute the sample with ethanol to 20W/V%,
The absorbance (transmittance) was determined in the same manner as in 5 above. Example 1 A continuous mother liquor circulation reaction was carried out using the reaction apparatus shown in FIG. Of the three reaction vessels used in the reactor, the first reaction vessel has a space that is 3/4 of the height from the liquid level to the ceiling of the reactor lid in the gas phase above the liquid level. The rotating plate rotates at the same speed as the stirring axis in a direction perpendicular to the stirring axis at a distance, and a portion of the liquid raw material to be supplied is supplied to the upper surface of the rotary plate,
In addition, a disk (outer diameter is 2/3 of the inner diameter of the reaction vessel) designed to allow the supplied liquid raw material to be injected onto the inner wall of the reactor by centrifugal force is installed on the stirring shaft. The temperatures of the first reaction tank, second reaction tank, third reaction tank, centrifugal separator, and anhydrous separator were each maintained at 50°C. In the first reaction tank, auxiliary acetone 24.6 g/hr, supplementary phenol 143 g/hr, 15% methyl mercaptan sodium aqueous solution 1.0 g/hr, circulating aqueous phase mother liquor 128
g/hr, supplemented with HCl gas at a rate of 5/hr. The circulating oil phase mother liquor was supplied at a rate of 269 g/hr near the center of the disk installed on the stirring shaft of the gas phase section above the liquid level of the first reaction tank, and was injected over the entire inner wall of the gas phase section. did. Here, the ratio of the injection supply liquid to the total supply liquid raw material is 0.48. A continuous reaction was carried out, and as a result, the slurry reaction mixture flowing out from the third reaction tank was intermittently charged into a centrifugal separator for solid-liquid separation. Regarding the separated aqueous phase mother liquor and oil phase mother liquor, an amount in excess of the predetermined amount to be supplied was extracted from the system, and the remainder was circulated to the first reaction tank and reused. The reaction conditions for this continuous reaction are summarized in Table 1.

[Table] The compositions of the circulating oil phase mother liquor and circulating water phase mother liquor in the continuous reaction were as shown in Table 2.

[Table] When this continuous reaction experiment was conducted for 350 hours, no solid matter was observed to adhere to the inner walls of the gas phase or gas-liquid interface in the reaction tank, and stable continuous operation was possible. Ta. In addition, circulating oil phase mother liquor and centrifuged cake [crude p, p'-BPA/PhOH]
The degree of coloration expressed as E ₄₈₀ changed over time as shown in FIG. This figure shows that the degree of coloration tends to increase with repeated mother liquor circulation.
Eventually, it will reach a plateau and will no longer increase. Similarly, the concentration of by-products in the oil phase mother liquor and centrifuged cake (crude p,p'-BPA/PhOH) also settled at a constant value. The by-products, HCl, H ₂ O concentration, and coloration degree contained in the oil phase mother liquor and centrifuged cake at this time were as shown in Table 3.

[Table] Also, the acetone conversion rate at the outlet of the third reaction tank is
99.5% p of acetone over 350 hours,
The total yield of p'-BPA/PhOH was 99.7 mol%. In addition, p, p′- obtained as a result of continuous reaction
Total average yield of BPA/PhOH is 146g per hour
It was hot. Example 2 In Example 1, the method of injecting the circulating oil phase mother liquor onto the inner wall of the reaction tank was changed by changing the rotary stirrer of the first reaction tank as follows, and the reaction conditions were exactly the same as in Example 1. A mother liquor circulation type continuous reaction was carried out using the following. A specific method for spraying and supplying the circulating oil phase mother liquor is to supply the oil phase mother liquor to the hollow stirring shaft of a rotary stirrer, and then inject it from a supply nozzle installed at the top of the reaction tank in the gas phase section of the reactor. , we used a method of washing the entire inner wall surface while rotating it. In this way, a continuous reaction experiment was carried out for 350 hours, and as with the results of Example 1, no solid matter was observed to adhere to the inner wall surface of the gas phase section of the reaction tank, and stable continuous operation was possible. did it. In addition, the recycled oil phase mother liquor and centrifuged cake after 350 hours of continuous reaction [crude p,p′-BPA・PhOH]
quality, change rate of acetone and p,p′-BPA・
The total yield of PhOH was exactly the same as in Example 1. Example 3 In Example 1, a continuous reaction was carried out for 350 hours by changing the injection feed liquid from the oil phase mother liquor to supplementary phenol. In this case, the ratio of the injection feed liquid to the raw material is 0.25. Continuous reaction was carried out in this manner for 350 hours, and as with the results of Example 1, no solid matter was observed to adhere to the inner wall surface of the gas phase section of the reaction tank, and stable continuous operation was possible. . In addition, the recycled oil phase mother liquor and centrifuged cake after 350 hours of continuous reaction [crude p,p′-BPA・PhOH]
quality, acetone conversion rate and p,p′-BPA・
The total yield of PhOH was exactly the same as in Example 1. Comparative Example 1 In the continuous reaction of Example 1, the reaction mother liquor was circulated under the same reaction conditions as in Example 1, except that the circulating oil phase mother liquor was not injected and supplied to the inner wall of the gas phase section in the reactor. Continuous experiments were conducted. Approximately 40 hours after the start of the continuous reaction, hard solids that had grown on the inner walls of the gas phase and the gas-liquid interface of the first reaction tank fell into the reaction mixture, and small pieces of solids fell into the reaction tank. It has accumulated inside. As a result, poor agitation and blockage of the overflow line were observed. Therefore, the supply of replenishing acetone, replenishing phenol, circulating mother liquor, etc. to the reaction system was stopped for 30 minutes, and the temperature inside the reaction tank was temporarily raised to 80°C to dissolve small pieces of solid matter. Then,
The mixture was slowly cooled to 50°C, returned to the original reaction temperature, and supply was started to resume continuous reaction. Thereafter, a continuous reaction was carried out for 350 hours in the same manner as in Example 1 while dissolving the solid matter at such intervals. As a result, E ₄₈₀ of the circulating oil phase mother liquor and centrifuged cake [crude p, p'-BPA/PhOH]
The degree of coloration, expressed as , changed over time as shown in Figure 3. As is clear from FIG. 3, the change over time of E ₄₈₀ settles down to a constant value after 300 hours or more, as in Example 1, but the degree of coloring is about three times as high as in Example 1. Table 4 shows the quality of the circulating oil phase mother liquor and centrifuged cake after 350 hours of continuous reaction. The total average yield of crude p,p'-BPA.PhOH obtained as a result of the continuous reaction was 141 g per hour.

[Table] As is clear from comparing the above examples, according to the present invention, better results can be obtained in terms of continuous operation time, yield, purity, etc. than in the case of the comparative example. This is an especially remarkable effect in mass-produced products such as the object of the present invention.

[Brief explanation of the drawing]

FIG. 1 is a system diagram of a mother liquor circulation type continuous condensation reaction apparatus used in one embodiment of the present invention. FIG. 2 shows the reaction time of circulating oil phase mother liquor and crude p,p'-BPA/PhOH in Example 1 of the present invention, and FIG. 3 shows the comparative example.
It is a graph showing the relationship with the degree of coloration at 480 nm. 1 and 2: Replenishment raw material tank, 3: Circulating oil phase mother liquor tank, 4: Circulating water phase mother liquor tank, 11-13:
Reaction tank, 14: Receiver, 15: Centrifugal separator, 16:
Anhydrous separator.

Claims (1)

[Claims] 1 consisting of reacting phenol and acetone in the presence of a soluble acidic catalyst to form a slurry reaction mixture containing crystals of a phenolic adduct of 2,2-bis(4-hydroxyphenyl)propane. In a method for producing a phenol adduct of 2,2-bis(4-hydroxyphenyl)propane, at least a part of the raw material supplied to the reactor is supplied to the reactor from a nozzle provided above the liquid phase surface of the reactor. A method for producing a phenol adduct of 2,2-bis(4-hydroxyphenyl)propane, characterized in that the reaction is carried out while spraying onto the inner wall of a phenol adduct of 2,2-bis(4-hydroxyphenyl)propane.