Process for the production of bisphenol A.

• US 5,324,867 A
• Filed: 07/13/1992
• Issued: 06/28/1994
• Est. Priority Date: 07/16/1991
• Status: Expired due to Term

• Current Assignee: Mitsubishi Chemical Corporation (Mitsubishi Chemical Group Corp.)
• Original Assignee: Chiyoda Corporation (Mitsubishi Corporation)
• Inventors: Yasui, Makoto, Watanabe, Tsuneo, Inaba, Ryuichi, Asaoka, Sachio, Yoneda, Noriyuki, Onda, Nobuhiro, Nishijima, Hiroaki, Shindo, Akio, Moriya, Nobuo, Imazeki, Takashi, Kukidome, Athumi, Shimogawara, Kaoru, Sakashita, Kouji, Maejima, Tetsuo
• Primary Examiner(s): Cintins, Marianne M.
• Assistant Examiner(s): PAGE, MARGARET
• Application Number:
  US07/912,487
• Time in Patent Office: 715 Days
• Field of Search: 568/724, 568/723, 568/727, 568/728
• US Class Current: 568/724
• CPC Class Codes: C07C 37/685 Processes comprising at least two steps in series
• CPC Class Codes: C07C 37/70 by physical treatment
• CPC Class Codes: C07C 37/84 by crystallisation
• CPC Class Codes: C07C 39/16 Bis-(hydroxyphenyl) alkanes; Tris-(hydroxyphenyl)alkanes

Abstract

High quality bisphenol A is produced from a neutral crystalline adduct of bisphenol A and phenol by fusing the adduct in an atmosphere having a maximum oxygen content of 0.005% by volume, followed by evaporation of liberated phenol. The crystalline adduct may be mixed with an aliphatic carboxylic acid before the fusion to reduce the coloring of the product. When an acidic crystalline adduct is used, the use of a strong alkali salt of an aliphatic carboxylic acid is suitably used. Interior surfaces of the apparatuses for carrying out the fusion and evaporation are desirably washed with an organic solvent to remove oxygen therefrom. The evaporation of phenol is suitably performed by two stage steam stripping wherein a used stripping gas obtained in the second stage is employed as a stripping gas in the first stage while steam is used as the stripping gas in the second stage.

Claims

1. A process of producing bisphenol A, comprising the steps of:

liquefying a crystalline adduct of bisphenol A and phenol to obtain a liquefied adduct containing bisphenol A and phenol;

feeding said liquefied adduct to an evaporating zone and forming said liquefied adduct into a downwardly flowing liquid film while maintaining said evaporating zone at a temperature of 160-185°

C. and a pressure of 15-60 Torr to vaporize and remove phenol from said liquefied adduct and thereby obtain a first product containing bisphenol A and 1-5% by weight of phenol;

introducing said first product into a first stripping zone and forming said first product into a downwardly flowing liquid film while feeding a stripping gas to said first stripping zone, wherein said liquid film of said first product is brought into counter-current contact with said stripping gas at a temperature of 170-185°

C. and a pressure of not higher than 15 Torr to strip phenol and to obtain a second product;

introducing said second product into a second stripping zone and forming said second product into a downwardly flowing liquid film while feeding steam to said second stripping zone, wherein said liquid film of said second product is brought into counter-current contact with said steam at a temperature of 170°

-185°

C. and a pressure of not higher than 15 Torr to strip phenol and thereby obtain a bisphenol A product and phenol-entraining steam; and

feeding said phenol-entraining steam to said first stripping zone as said stripping gas.

2. A process as claimed in claim 1, wherein said crystalline adduct has an APHA color of 15 or less.

3. A process as claimed in claim 1, further comprising the steps of:

`discharging said stripping gas which has been contacted with said first product and which entrains phenol and bisphenol A from said first stripping zone;

introducing said discharged stripping gas into a first cooling zone maintained at a pressure of 30 Torr or less and such a temperature that steam is prevented from condensing while a portion of said phenol is condensed, wherrein said discharged stripping gas is brought into counter-current contact with a first liquid cooling medium to condense substantially all of said bisphenol A and part of said phenol and thereby obtain a mixed gas containing uncondensed steam and uncondensed phenol, said first liquid cooling medium being phenol or bisphenol A containing phenol; and

introducing said mixed gas into a second cooling zone maintained at a pressure of 30 Torr or less and such a temperature that substantially all of said mixed gas is condensed, wherein said mixed gas is brought into counter-current contact with a second liquid cooling medium to condense substantially all of said mixed gas and thereby obtain a condensate-containing liquid, said second liquid cooling medium being an aqueous solution of phenol.

4. A process of producing bisphenol A, comprising the steps of:

liquefying a crystalline adduct of bisphenol A and phenol, which has an APHA color of not greater than 15 and which shows a pH of 4.9-5.5 when dissolved in an aqueous methanol solution having a pH of 5, to obtain a liquefied adduct containing bisphenol A and phenol;

feeding said liquefied adduct to an evaporating zone and forming said liquefied adduct into a downwardly flowing liquid film while maintaining said evaporating zone at a temperature of 160°

-185°

C. and a pressure of 15-60 Torr and in an atmosphere having an oxygen concentration of 0.005% by volume or less to vaporize and remove phenol from said liquefied adduct and thereby obtain a first product containing bisphenol A and 1-5% by weight of phenol;

introducing said first product into a first stripping zone and forming said first product into a downwardly flowing liquid film while feeding a stripping gas to said first stripping zone, wherein said liquid film of said first product is brought into counter-current contact with said stripping gas at a temperature of 170-185°

C. and a pressure of not higher than 15 Torr to strip phenol and to obtain a second product;

introducing said second product into a second stripping zone and forming said second product into a downwardly flowing liquid film while feeding steam to said second stripping zone, wherein said liquid film of said second product is brought into counter-current contact with said steam at a temperature of 170-°

185°

C. and a pressure of not higher than 15 Torr to strip phenol and thereby obtain a bisphenol A product and phenol-entraining steam; and

feeding said phenol-entraining steam to said first stripping zone as said stripping gas.

5. A process as claimed in claim 4, further comprising mixing said liquefied adduct with an alarphatic carboxylic acid to obtain a mixture containing 1-100 ppm of the aliphatic carboxylic acid based on the weight of said adduct, said mixture being then fed to said evaporating zone.

6. A process as claimed in claim 4, wherein said crystalline adduct has been subjected to recrystallization from phenol and washed with purified phenol.

7. A process as claimed in claim 4, further comprising the steps of:

discharging said stripping gas which has been contacted with said first product and which entrains phenol and bisphenol A from said first stripping zone;

introducing said discharged stripping gas into a first cooling zone maintained at a pressure of b 30 Torr or less and such a temperature that steam is prevented from condensing while a portion of said phenol is condensed, wherein said discharged stripping gas is brought into counter-current contact with a first liquid cooling medium to condense substantially all of said bisphenol A and part of said phenol and thereby obtain a mixed gas containing uncondensed steam and uncondensed phenol, said first liquid cooling medium being phenol or bisphenol A containing phenol; and

introducing said mixes gas into a second cooling zone maintained at a pressure of 30 Torr or less and such a temperature that substantially all of said mixed gas in condensed, wherein said mixed gas is brought into counter-current contact with a second liquid cooling medium to condense substantially all of said mixed gas and thereby obtain a condensate-containing liquid, said second liquid cooling medium being an aqueous solution of phenol.

8. A process as claimed in claim 6, wherein said purified phenol is obtained by:

providing a raw material phenol which contains an impurity forming a high boiling point material having a boiling point of higher than 185°

C. upon being heated at a temperature higher than the melting point of phenol and which has a water content of not greater than 0.5% by weight,

contacting said raw material phenol with a strong-acid ion exchange resin at such a temperature as to convert at least part of said impurity into said high boiling point material and to obtain treated phenol; and

distilling said treated phenol at a temperature of 185°

C. or less to separate purified phenol as distillate from said high boiling point material.