• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A novel process for producing isopropenyl phenol such as p-isopropenyl phenol which comprises continuously feeding oligomers of isopropenyl phenol having a degree of polymerization of 2 to 5 into a high-boiling inert organic reaction medium such as an alkylnaphthalene heated at 150 DEG to 250 DEG C. under a pressure of 10 to 100 mmHg while maintaining the concentration of the oligomers in the reaction medium at not more than 30% by weight, thereby thermally decomposing the oligomers in the reaction medium; and continuously distilling off the resulting isopropenyl phenol out of the reaction system and recovering it. The process almost quantitatively gives isopropenyl phenol having reduced contents of impurities.
    公开号:SU976844A3
    申请号:SU792802902
    申请日:1979-08-14
    公开日:1982-11-23
    发明作者:Като Нобукацу；Таказе Цутоми；Моримото Есио；Юаса Теруо；Хаттори Минору
    申请人:Мицуи Тоацу Кемикалз Инк (Фирма)；
    IPC主号:
    专利说明:

    (54) METHOD OF OBTAINING P-ISOPGYUPENILPHENOL
    one
    This invention relates to methods for producing n-isopropenylphenol and can be used as an intermediate for the production of bisphenol A.
    A known method of producing isopropanylphenol by alkylation of benzene with propylene, oxidizing the resulting mixture of p- and m-diisopropylbenzene to obtain a mixture of p-and m- (2-hydroperoxypropane 1-2) cumene, which is cleaved at 10 O13 in the presence of acid catalyst 1.
    However, this method is technologically difficult due to the presence in the 4et Koft technology of the three stages of isopropenylphenol production.
    The closest in technical essence to the present invention is a method for producing α-isopropenylphenol by thermal cleavage of p-isopropenylphenol oligomers at 15 O-25 O ° C and a pressure of 1 O-500 mm Hg. Art. with the subsequent release of the target product we obtained vapors by absorption of sfga1
    KIM solvent, such as gltcol, n-ether. 15 yield of the desired product 91-96.8% 21
    The disadvantage of this method is that the yield of the desired product is not high enough (01-96.8%).
    The purpose of the invention is to increase the yield of the target product.
    This goal is achieved by the method of obtaining p-isopropenylphenol by thermal melting of 2–3 O% solutions of p-isopropenylphenol oligomers at 15 ° –25 ° C and a pressure of 101OO mm Hg. in the environment of organic matter selected from the group; including C-C d-alkylnaphthalenes with the number of alkyl radicals 1-3, VAT residue from the distillation of diphenylolpropane, novolac resin with t, size. 60-150 C.
    In order to split the oligomers of p-isopropenylphenol by the thermal method proposed, it is necessary to heat the inert organic reaction medium to a temperature sufficient for a smooth decomposition of 3976 years of isopropenylphenol oligomers to p-isopropenylphenoosh. Typically, this temperature is preferably in the range of 150-250 ° C. When the temperature of the inert organic reaction medium is lower than that, the rate of thermal dissociation of the igomers n-isopropenylphenol decreases and, accordingly, the rate of distillation of the split product from the reaction system decreases. Moreover, part of the oligstlerov p-isopropenylphenol is distilled in a non-split state and is mixed with the split product, reducing its purity. When TOMneparjpa of an inert organic reaction medium is higher than 250 ° C, side reactions occur, such as dealkylation of the resulting n-isopropene of phenol or conversion of the starting material and / or the melted product into a resin, and therefore the yield and purity of the product are reduced. The temperature lnapaon 20O-24OC 1U1 is most preferable, because within this rate (of the working range, the formation of byproducts decreases and thawing proceeds smoothly. After the formation of the thermally split product, it should be distilled off from the reaction system. the reaction system or the inert organic reaction medium must be T1ls under reduced pressure. The degree of pressure decrease varies depending on the cleavage temperature, but usually the reception The range is 10-100 mm Hg. When the pressure is lower than Y ivtM Hg, a part of the opigomers of the n -isopropole of schlphenol or a part of the inertial organic reaction medium are distilled with the thermally split product and mixed with it in this way reducing the purity of the product. When 1 pressure is higher than 1OO mmHg, it is difficult to distil the thermally split product from the reaction system. This prolongs the residence time of the product in the reaction system and gives side reactions, such as conversion of P-iso propenylphenol into pitch and its colors ation. As a result, the yield decreases and the purity of the product decreases with the inclusion of by-products in the desired product. To conduct a reaction smoothly because of the rapid distillation of the thermally split product from the reaction system, the pressure is preferably about 50-100 mm Hg. Art. in particular, preferably 50-70 mm wg. Art. For TefiKniMccKoro to melt n-isopropylphenol oligoers at a specified temperature and pressure, the organic reaction medium is a high boiling inert organic solvent that has a melting point or cleavage no more than 15 ° C and vapor pressure lower than vapor pressure resulting from n isopropenylphenol at the temperature of cleavage of oligomers of p-isopropenylphenol. More acceptable is a high boiling inert organic solvent having a vapor pressure at 25 ° C of not more than 1OO mm Hg. Art. Examples of such solvents are hydrocarbon-type heat transfer media, such as alkyl naphthalenes (KSK-OtP and T4e0 SK-Oi 8 available as commercial products, manufactured by Sauken Kagaku Co., Inc.), alkyl naphthalene refers to naphthalene having 1-3 alkyl substituents. The substituent may be in the (L- or p-position, i.e. there are no restrictions on the number of carbon atoms contained in the alkyl group. The bottom residue after distillation of diphenylolpropane (bisphenol A) is a tar (tar-like) substance consisting of mixtures of polydermal condensed aromatic substances that are not distilled (does not produce distillate) even under heating conditions at 2OO-250 ° C and a residual pressure of 2-1O mm Hg. The bottom residue after the distillation column of bisphenol A includes, in wt.% : Bisphenol Isomers A 1-36; chroman compound (general purpose chroma 1) 1-1 O; polyphenolic compound with 2-6 drami and resin-like high molecular weight substance 99-6 O. The molecular weight of the polyfenome compound and resinous high molecular weight substance is in the ZOO-ZOOO limit. Novolac resin of the phenolic resin type, having a softening temperature of 6О-15ОС 31S K-2531 / 3IS (Japan standards) was obtained by condensation of formaldehyde with an excess of phenol or cresol in the presence of acid. - A novolac-type fenoshene resin is obtained by removing low boil pshh (i.e. bale, below 12 ° C at 10 mm Hg) from the product formed during phenol decontamination, such as phenol or cresol, with formaldehyde at a molar ratio of formaldehyde / phenol not less than 1.0. . A new-type phenolic resin has a number average molecular weight of 400-2000 or a weight-average molecule having a pk weight of 1000-500 O. The degree of branching is 5-20%. The inert organic reaction medium used in the proposed invention dissolves the oligomers of P-isopropenylphenol at 15 ° C-250 ° C well. Thermal splitting of the p-isopropenylphenol oligomers is carried out by feeding the reaction medium to a reactor equipped with an inlet feed, an opening for the initial oligomers. p-iipropenylphenol and a distillation outlet for p-isopropenylphenol as a thermally split product and optionally a stirrer. The reaction medium is maintained at a high temperature, preferably at 150-250 ° C and a pressure of 10-1OO mm Hg. and feed the original opigomers with isopropylphenop into the reactor. Thus, the supplied oligome (P-vopropenylphenol is dissolved in the reaction mixture and thermally expanded to P-vopropenylphenode in the liquid phase. Blend the products 6i icTpo distilled from the reaction system. (D the rate that the concentration of oligomers in the reaction medium is maintained at no more than 30% by weight. If the oligomers of P-vopropenylphenol are fed at such a high speed that the concentration of the opnomer exceeds 30% by weight, then the feed will be The amount of heat to distill the split product becomes difficult in this thermal decomposition reaction, which requires such a large amount of energy. As a result, the amount of thermally split product that is produced in the reaction system is reduced and its conversion to the resin continues to reduce the yield P-isopropenylphenol. The thermal cleavage of the starting material and the distillation of the cleaved Drozukg are particularly smooth and a good result is obtained when the concentration of Homer l-isopropenylpheno and in the reaction medium is 2-15% by weight. 46 The concentration of oligomorphs p-isopropenylphenol E to the reaction medium can be determined by, for example, gas chromatography. The mixing of the starting material in the reaction medium can be carried out in the usual mechanical way, for example, mixing the reaction mass with bubbles of an inert gas such as nitrogen, carbon dioxide, helium or argon. This leads to a stirring of the reaction medium and makes the splitting of the p-isopropene: xphenol opomers smooth. Moreover, it facilitates the removal of p-isopropenylphenol from the reaction system. The p-isopropenylphenol distilled from the reaction system can be recovered by cooling to condense it to a liquid or solid state, or by dissolving it without condensation immediately after condensation in a high boiling polar solvent such as 2-ethylhexanol. Thus, the resulting p-isopropenylphenol is used as a material for various or-. panic syntheses. The use of the invention allows to increase the yield of the target product to 97.5-99.1%. Example 1. A reactor (volume 1 l), equipped with a feed opening, an outlet for distilling the split product, an inlet pipe (sparging tube) for introducing an inert gas and a thermometer, load 85 g (liquid depth 3.1 cm) of K5K alkylnaphthalenes - OiP (product of the firm Sauk Kagaku Co., Inc.). The temperature of the reaction medium is raised to 24 ° C, the pressure inside the reactor is maintained at 5 ° mm Hg. Art. Oligomers of p-isoprbcenylphenol are continuously fed. . in the KSK-on, through the x-hole, to supply a single material at a speed of 35 O g / h and gas of a speed of 4.3 l / min is injected from the inlet pipe and bubbled through K9K-SCH2. As a result, the thermally split product is continuously distilled from the reactor, cooled, condensed and collected. During thermal cleavage, the concentration of oligomers of p-isoprotic Elphenol in K5K - OiC is maintained with an average of 10 wt.%. The above reaction is carried out for 10 hours in order to cleave the 3,5OO ligomers of p-isoypenylpheno a. Get 3,43O g (yield 98, O%)
    P-ipopropenylphenol, with a purity of 94.1%.
    . Example 2, The same reactor as in Example B is charged with 80 g (liquid depth 2.9 cm) of the cubic residue from distillation of bisphenol A. With the same conditions as described in the example, 1.3 SQO g is split. oligomero p-aaopropeniphenol. The concentration of the opigomers p-isopropenlphenop in the reaction mixture is maintained at 10.5 wt.%.
    3.47 O g (yield 99.1%) of p-isopropenylphenol are obtained, having a purity of 93.0%.
    Example 3. The same reaction as in example 1 was charged with 80 g (liquid depth 2.9 cm) of a novolak resin having a softening point determined by E15K-2531,.
    Under the same conditions as in Example 1, 3500 g of p-isopropenylphenop oligomers are cleaved. In time
    The resulting yield and purity of the final product p-isopropenylphenol are given in table. 2
    Table 2
    by thermal cleavage of the concreting oligomers of p-isopropylphenol in the reaction medium was maintained at 10.5 wt.%.
    3.488 g (yield 98.5%) of P-isopropenylphenol are obtained, having a purity of 92.9%.
    Examples 4-8. In the same reactor used in the example, 80 g (liquid depth 2.9 cm) of the cubic residue is loaded, from distillation of bisphenol A. The oligomers of n-isopropenylphenol are split under the conditions given in table. 1, in which the thermal cleavage temperature refers to the temperature of the residue at. distillation of bisphenol A, and the pressure of thermal decomposition to the pressure inside the reactor. During thermal decomposition, gaseous nitrogen is introduced at a rate of 4.3 liters / min through the gas inlet pipe and bubbled through the bottom residue from distillation of bisphenol A.
    Table
    PRI me R 9 (comparative) Use the same peakTop as in
    example 1. Inside the reactor Lodderzhayuyag temperature and pressure of 50 mm RT, Art. Without the use of the reaction medium (solvent), n-isopropenylphenol oligomers are continuously added through
    Blend the inlet at a rate of 35 O g / h for 2 hours and split under the same conditions as in Example 1 .;
    . 460 g (yield 65.7%) of rhizopropenylphenol having a purity of 80.2% are obtained.
    Example 1O (comparative). 1OOO g opigrmerov p- -isopropenylpheno
    权利要求:
    Claims (1)
    [1]
    Claim
    25 The method of producing p-isopropenylphenol by thermal decomposition of oligomers of p-isopropenylphenol at a temperature of 150-250 ° C and a pressure of ΙΟΙ 00 mm RT. Art., otlichayuschiyEO with I in that in order to increase the yield of the desired product, is subjected to cleavage of 2-30% solutions of oligomers:, PV-izopropenilfenola.v organic solvent selected from the group: conductive vklyuchayu35 C ^ -C 10 - alkyl naphthalenes with the number of alkyl radicals 1-3, the bottom residue from the distillation of diphenylolpropane, novolac resin with a softening point of 60-150 ° С.
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    同族专利:
    公开号 | 公开日
    NL181731C|1987-10-16|
    AU4947279A|1980-02-21|
    JPS5811930B2|1983-03-05|
    CA1145364A|1983-04-26|
    IN152042B|1983-10-01|
    DD145528A5|1980-12-17|
    CH642042A5|1984-03-30|
    DE2932959A1|1980-02-28|
    ES483402A1|1980-04-16|
    YU40573B|1986-02-28|
    FR2433502A1|1980-03-14|
    US4242528A|1980-12-30|
    GB2028812A|1980-03-12|
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    IT1122386B|1986-04-23|
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    GB2028812B|1982-11-03|
    CS213392B2|1982-04-09|
    YU188979A|1982-08-31|
    AR221099A1|1980-12-30|
    BE878234A|1979-12-03|
    FR2433502B1|1984-02-10|
    NL181731B|1987-05-18|
    IT7924830D0|1979-08-01|
    HU182536B|1984-02-28|
    MX150934A|1984-08-22|
    AU524695B2|1982-09-30|
    BR7905157A|1980-07-15|
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    引用文献:
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    FR69895E|1956-01-31|1959-01-09|Distillers Co Yeast Ltd|Improvements in the recovery of phenols|
    DE1235894B|1959-08-18|1967-03-09|Bayer Ag|Process for the preparation of alkenylphenols from dihydroxydiarylalkanes|
    GB903062A|1959-11-25|1962-08-09|Ciba Ltd|Dimeric p-isopropenylphenol, a process for its production and its use in the preparation of 1:3:3:trimethyl-1-p-hydroxyphenyl-indan-6-ol|
    JPS5652886B2|1973-08-10|1981-12-15|
    PL103054B1|1976-09-12|1979-05-31|Instytut Ciezkiejsyntezy Organic|METHOD OF PROCESSING WASTE FROM THE PROCESS OF MANUFACTURING DIPHENYLOLPROPANE|US4260831A|1978-04-03|1981-04-07|Sumitomo Chemical Company, Limited|Oligomerization of m-isopropenylphenol|
    FR2470106A1|1979-11-22|1981-05-29|Mitsui Toatsu Chemicals|Hydroxy-indene cpds. - useful as in prepn. of carbamate and organo-phosphate agrochemicals, and as starting material for novolak resins|
    US4405818A|1981-09-30|1983-09-20|Mobil Oil Corporation|Production of meta-isopropylphenolic products|
    US4594459A|1985-03-25|1986-06-10|The Dow Chemical Company|Preparation of p-isopropenyl phenol and related compounds|
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    DE3721853A1|1987-07-02|1989-01-12|Bayer Ag|METHOD FOR PRODUCING MONOMERAL ALKENYLPHENOLS FROM DIHYDROXYDIPHENYLALKANES|
    US6012530A|1997-01-16|2000-01-11|Korsgaard; Jens|Method and apparatus for producing and shipping hydrocarbons offshore|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP53098721A|JPS5811930B2|1978-08-15|1978-08-15|
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