WO2004035512A1 - ビスフェノールaの製造方法 - Google Patents
ビスフェノールaの製造方法 Download PDFInfo
- Publication number
- WO2004035512A1 WO2004035512A1 PCT/JP2003/013184 JP0313184W WO2004035512A1 WO 2004035512 A1 WO2004035512 A1 WO 2004035512A1 JP 0313184 W JP0313184 W JP 0313184W WO 2004035512 A1 WO2004035512 A1 WO 2004035512A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- phenol
- bisphenol
- adduct
- filter
- layer
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/70—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment
- C07C37/84—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by crystallisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/11—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions increasing the number of carbon atoms
- C07C37/20—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions increasing the number of carbon atoms using aldehydes or ketones
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C39/00—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring
- C07C39/12—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring polycyclic with no unsaturation outside the aromatic rings
- C07C39/15—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring polycyclic with no unsaturation outside the aromatic rings with all hydroxy groups on non-condensed rings, e.g. phenylphenol
- C07C39/16—Bis-(hydroxyphenyl) alkanes; Tris-(hydroxyphenyl)alkanes
Definitions
- the present invention relates to a method for producing bisphenol A [2,2-bis (4-hydroxyphenol) pulp bread], and more particularly to a method for separating an adduct of bisphenol A and phenol in the production method. It is. Background art
- Bisphenol A is known to be an important compound as a raw material for engineering plastics such as polycarbonate resin and polyarylate resin, or epoxy resin, and its demand has been increasing in recent years. is there.
- This bisphenol A is produced by condensing excess phenol and acetone in the presence of an acidic catalyst and optionally a cocatalyst such as a sulfur compound.
- Bisphenol A can be extracted from the reaction mixture by directly separating it from the reaction mixture in the form of crude crystals, or by concentrating and cooling the liquid mixture after removing acetone, water, etc. from the reaction mixture.
- a method is known in which an adduct of A and phenol is precipitated and separated.
- the mainstream method is to separate and separate the latter adduct of bisphenol A and phenol.
- the adduct of bisphenol A and phenol is crystallized, and the crystals are separated from the mother liquor by a known solid-liquid separation method using filtration or a centrifuge (for example, see 5 7-7 7 6 3 7 Publication, Japanese Unexamined Patent Publication No. Hei 5-3131088, Japanese Unexamined Patent Publication No. Sho 63-2757539, Japanese Unexamined Patent Publication No. Hei 6-3600 No. 2).
- the suction type belt filter is used for the separation by the filtration method.
- a tray filter, a drum filter, etc. can be used (for example, see Japanese Patent Application Laid-Open No. Hei 7-25798, page 3 [0011]). It is necessary to make large crystals and reduce the surface area in order to prevent or purify them (for example, see Japanese Patent Application Laid-Open No. 5-31088).
- the method using a centrifuge is preferable in order to reduce the liquid content between crystals and obtain a more dried adduct.However, since the centrifugal load is applied, the crystals are crushed and the efficiency of replacement of the mother liquor and washing solution is reduced. It is worse than the filtration method. Therefore, processing a large amount of products
- the present inventors have conducted intensive studies on a method for producing bisphenol A having the above-mentioned problems. By introducing a heated inert gas stream and operating the belt filter under specific conditions, the adduct of bisphenol A and phenol can be continuously and efficiently stabilized. And found that it can be recovered with high purity, and reached the present invention.
- the present invention provides the following method for producing bisphenol A.
- a phenol slurry solution of bisphenol A containing an adduct of bisphenol A and phenol in a crystalline state is introduced under reduced pressure into a heated inert gas stream over a horizontal endless belt filter.
- an adduct layer of crystalline bisphenol A and phenol is formed on the filter,
- the liquid content of the adduct layer is 30% by weight. / 0 or less
- a process for producing bisfunol A comprising:
- a horizontal endless belt filter is used in the solid-liquid separation in the steps (D) and (D '), and the belt filter is operated under specific conditions.
- a horizontal endless belt filter is used in the solid-liquid separation in the steps (D) and (D ′), and a slurry solution containing an adduct of bisphenol A and phenol in a crystalline state is added under reduced pressure.
- a heated inert gas in a low-oxygen atmosphere is introduced, and oxygen contained in the adduct is effectively removed, so that a higher-quality bisphenol is obtained.
- an acidic catalyst an acid type ion exchange resin can be used.
- the acid-type ion exchange resin is not particularly limited, and those conventionally used as a catalyst for bisphenol A can be used. Fats are preferred.
- the sulfonic acid type cation exchange resin is not particularly limited as long as it is a strongly acidic cation exchange resin having a sulfonic acid group.
- sulfonated styrene-dibutylbenzene copolymer sulfonated crosslinked styrene polymer, phenol honolaldehyde sulfonic acid Acid resin, benzene formaldehyde monosulfonic acid resin and the like. These may be used alone or in combination of two or more.
- Lukabutanes are used in combination.
- This mercaptan refers to a compound having a SH group in a free form in a molecule, and has such a compound as an alkyl mercaptan or one or more substituents such as a carboxyl group, an amino group, and a hydroxy group.
- Alkyl mercaptans for example, mercaptocarboxylic acid, aminoalkanethiol, mercaptoalcol, and the like can be used.
- mercaptans examples include thiocarboxylic acids such as methyl mercaptan, ethyl mercaptan, n-butylglycolic acid,] 3-mercaptopropionic acid, aminoalkanethiols such as .2-aminoaminothiol, Examples thereof include mercapto alcohols such as mercaptoethanol, and among them, alkyl mercaptans are particularly preferable in view of the effect as a cocatalyst. These mercapdans may be used alone or in combination of two or more. These mercaptans can be immobilized on the acid-type ion exchange resin to function as a catalyst. -The amount of the mercaptans used is generally from 0.1 to
- 2 0 mole 0/0 preferably, is selected in the range of 1 to 0 mole 0/0.
- reaction solvent is generally not required, except that the reaction solution has a too high viscosity or reacts at a low temperature at which solidification makes the operation difficult.
- the condensation reaction between phenol and acetone may be either a batch type or a continuous type.
- a reaction tower filled with an acid-type ion-exchange resin phenol, acetone and mercaptans (mercaptans are acid-type ion exchange resins)
- mercaptans are acid-type ion exchange resins
- the number of reaction towers may be one, or two or more may be arranged in series.
- industrially it is particularly advantageous to employ a fixed-bed multistage continuous reaction system in which two or more reaction towers filled with an acid-type ion exchange resin are connected in series.
- the acetone / phenol molar ratio is usually selected in the range of 1/3 0 to 1/3, preferably 1/15 to 1/5. If the molar ratio is less than 1/30, the reaction rate may be too slow. If the molar ratio is more than 1/3, the generation of impurities tends to increase, and the selectivity of bisphenol A tends to decrease.
- the molar ratio of the mercaptans to Zaceton is usually selected from the range of 0.1Z100 to 20/100, preferably 1Z100 to 10/1/1.
- the molar ratio is less than 0.1 / 100, the effect of improving the reaction rate and the selectivity of bisphenol A may not be sufficiently exhibited. If the molar ratio is larger than 20Z100, the effect is not much improved in proportion to the amount. I can't.
- the reaction temperature is selected in the range of usually 40 to 150 ° C, preferably 60 to 11'0 ° C. If the temperature is lower than 40 ° C, the reaction rate is low and the viscosity of the reaction solution is extremely high, and in some cases, there is a risk of solidification. If the temperature exceeds 150 ° C, reaction control becomes difficult, and The selectivity of phenol A (integrated with ⁇ and ⁇ ') decreases, and the acid type ion exchange resin of the catalyst may decompose or deteriorate. Further, the LHSV (liquid hourly space velocity) of the raw material mixture is usually 2 to 30 hr, preferably 0.1 hr.
- the reaction mixture containing bisphenol A obtained in the reaction step (A) is substantially free of an acid-type ion-exchange resin, that is, in the case of a batch reaction method.
- the catalyst is removed by filtration or the like, and in the case of a fixed bed continuous reaction system, a low-boiling substance removal treatment is performed as it is.
- This vacuum distillation is generally carried out at a pressure of 6.5 to 80 kPa and a temperature of 70 to 180 ° C. Will be implemented. At this time, unreacted phenol azeotropes, and a part of the azeotrope is removed from the distillation column to the outside of the system together with the low-boiling substances.
- the temperature of the heating source used is preferably set to 190 ° C. or less in order to prevent the thermal decomposition of bisphenol A.
- SUS304, SUS316 and SUS316L are generally used as materials for the equipment.
- the bottom liquid from which the low-boiling components have been removed from the reaction mixture contains bisphenol A and phenol.
- the phenol is distilled off under reduced pressure to concentrate bisphenol A. There are no particular restrictions on the concentration conditions.
- the concentration of bisphenol A in the concentrate is preferably 20 to 50% by weight. / 0 , good. 20 ⁇ 40 weight. It is in the range of / 0 . If this concentration is less than 20% by weight, the recovery of bisphenol A is low,
- a 1: 1 adduct of bisphenol A and phenol (hereinafter sometimes referred to as phenol adduct) is obtained from the concentrated liquid obtained in the concentration step of step (C). This is the process of crystallization and separation.
- the concentrated liquid is cooled to about 40 to 70 ° C., and phenol adduct is crystallized to form a slurry.
- the cooling at this time may be carried out using an external heat exchanger, or may be carried out by adding water to the concentrated liquid and cooling by utilizing the latent heat of evaporation of water under reduced pressure. Good.
- this vacuum cooling crystallization method about 3 to 20% by weight of water is added to the concentrated solution, and crystallization treatment is performed under the conditions of a normal temperature of 40 to 70 ° C and a pressure of 4 to 16 kPa. Is performed.
- the amount of water is less than 3% by weight, the heat removal ability is not sufficient, and if it exceeds 20% by weight, the dissolution loss of bisphenol A increases, which is not preferable.
- the crystallization temperature is lower than 40 ° C, the viscosity of the crystallization liquid may increase and solidification may occur. If the crystallization temperature exceeds 70 ° C, the dissolution loss of bisphenol A increases.
- the slurry containing the crystallized phenolic adduct is introduced into a horizontal endless belt filter (also simply referred to as a belt filter) in a heated inert gas stream under reduced pressure.
- a horizontal endless belt filter also simply referred to as a belt filter
- An adduct layer of bisphenol A and phenol in a crystalline state is formed on the filter.
- the horizontal endless belt filter is a filter that supports a filter cloth with a porous endless conveyor and runs over a vacuum box, supplies slurry to one end, and performs filtration and cake washing. Separated. .
- Horizontal endless belt filter A porous sheet made of polypropylene, polyester, nylon, polytetrafluoroethylene, cotton cloth, linen cloth, etc. is used for one filter cloth.
- the use of a horizontal endless belt filter is advantageous because the filtration can be continuously performed and the filtration can be performed without applying a large gravity.
- the average particle size of the adduct of bisphenol A and phenol in a crystalline state is 0.05 to 1 mm. If the average particle size is less than 0.05 mm, it becomes difficult to separate the phenol adduct crystals from the mother liquor, and clogging of the filter medium occurs, resulting in a reduction in treatment efficiency. If it is larger than 1 mm, there is a risk that mother liquor may enter the crystal.
- Nitrogen gas is usually used as the inert gas, and the oxygen concentration in the nitrogen gas is 5 OO O pp or less, preferably 300 ppm or less.
- the liquid content of the adduct layer was 30% by weight. / 0 or less, preferably 2.5% or less.
- the liquid content of the adduct layer needs to be 30% by weight or less, and the adduct layer contains adducts deposited on the filter. The lower the liquid fraction, the less the load on subsequent processes.
- the mother liquor can be separated from the phenol adduct crystals by filtration under reduced pressure, and the liquid content of the adduct layer can be reduced.
- the preferred degree of pressure reduction is 60 to 95 kPa.
- the liquid content of the adduct layer is adjusted by adjusting the degree of pressure reduction and the belt speed of the horizontal endless belt filter. It can be 30% by weight or less.
- the thickness of the adduct layer is not limited as long as the deposited phenol product having a liquid content of 30% by weight or less is formed on the belt filter, but if it is too thick, the weight per unit area increases, and It is not preferable because the load is increased.
- phenol, water, a mixed solution of water and phenol, or a solution in which bisphenol A is dissolved is used.
- the thickness of the adduct layer and the time of suction under reduced pressure can be adjusted by the belt speed.
- the temperature must be 80 ° C or lower to maintain the slurry containing the phenol adduct crystallized during filtration, and the temperature of the atmosphere containing the filter may be reduced because solidification of the mother liquor and washing solution may occur. It is important to keep the temperature at 30 to 80 ° (preferably 35 to 5.0 ° C).
- the separated mother liquor can be directly or partially recycled to the reactor, or partially or wholly isomerized and recycled to the crystallization raw material.
- the phenol adduct that has been crystallized in the CD) process is dissolved using a phenol-containing solution.
- the phenol-containing solution used in this step is not particularly limited.
- the above-mentioned phenol-containing solution is added to the phenol adduct crystals obtained in the step (D), and the mixture is heated to about 80 to 110 ° C, and the phenol adduct is heated and dissolved to perform a crystallization operation.
- a bisphenol A-containing solution having a preferred bisphenol A concentration is prepared.
- the bisphenol A-containing solution thus prepared has a low viscosity even at relatively low temperatures and is relatively easy to handle, and is suitable for filtration through a filter.
- the phenol adduct is crystallized from the bisphenol A-containing solution, solid-liquid separated, the phenol adduct is dissolved using the phenol-containing solution, and then the crystallization and solid-liquid separation in step (D) are performed. Repeat at least once.
- the heating and melting step is a step of heating and melting the phenol duct separated and crystallized in the above step (D) or (D '). In this step, phenol adak is heated and melted at about 100 to 160 ° C. to form a liquid mixture.
- the dephenol removal step is a step in which phenol is distilled off from the phenol duct heated and melted in the step (E) by vacuum distillation to recover the bisphenol A in a molten state.
- the vacuum distillation is generally carried out under the conditions of a pressure of 1.3 to 13.3 kPa and a temperature of 150 to 190 ° C. Residual phenol can be further removed by steam stripping.
- the bisphenol A in a dissolved state obtained in the above step (G) is formed into droplets by a granulation device such as a spray dryer, and then cooled and solidified to obtain a product.
- the droplets are formed by spraying, spraying, etc., and cooled by nitrogen, air, or the like.
- the feature of the method for producing bisphenol A of the present invention is that the solid-liquid separation in the steps (D) and (D ') is carried out using a suction belt filter and heating After introducing the active gas stream and separating the mother liquor through the filter, the phenol duct is separated by its own weight, whereby the adduct of bisphenol A and phenol is stably and continuously added. It can be recovered efficiently and with high purity.
- the adduct crystals separated from the mother liquor formed a layer 82 mm thick.
- the liquid content of the wet adduct was determined to be 24.5% by weight.
- the substitution rate of the mother liquor was 98.7% as determined from the isomer content by liquid chromatography.
- the resulting adduct was melted, and the Hazen color number was measured at 175 ° C for 20 minutes. The result was APHA5.
- the CCS of the air permeability is an abbreviation of ccZcm / sec, and indicates the amount of air ( CC ) that passes through the filter cloth per unit area (lcm) per unit time (1 second).
- step (A) a reactor filled with 600 g of a cation exchange resin was heated at a rate of 75 g at a rate of 4600 g / hr of phenol, 280 g / hr of acetone, and 16 g / hr of ethyl methyl carbbutane. It was supplied continuously while maintaining at ° C.
- the reaction mixture is sent to the low-boiling substance removal step (B) to remove low-boiling substances mainly including unreacted acetone, and to obtain a reaction product mainly including bisphenol A and unreacted phenol at 4640 g / hr. Was done.
- step (C) phenol was partially removed from the reaction product at 165 ° C and 53.3 kPa (400 Torr) to reduce the concentration of bisphenol A. It concentrated adjusted to be 30 wt 0/0. Water was added to the bisphenol A concentrate, and the mixture was cooled and crystallized under stirring at 45 ° C. to crystallize an adduct of bisphenol A and phenol.
- the mixture was poured into a Nutsche lined with propylene filter cloth (Daiwa Spinning Co., Ltd., air permeability 70 CCS), and separated into mother liquor and crystals of an adduct of bisphenol A and phenol. After washing phenol (about 0.75 times the wet cake) was poured into the adduct crystals separated from the mother liquor, suction was continued for about 15 seconds.
- the adduct was formed into a cake having a thickness of 64 mm, and the cake of the adduct was taken out by cutting the cake and applying a slight impact.
- the liquid content of the obtained adduct was measured and found to be 25.2%. Further, the substitution rate of the mother liquor was determined by liquid chromatography from the content of the isomer, and as a result, was 99.1%.
- the resulting adduct was melted, and the Hazen color number was measured at 175 ° C for 20 minutes. As a result, it was APHA5. As described above, it can be seen that Example 1 can be reproduced using Nutsche.
- Example 2 The procedure was performed in the same manner as in Example 1 except that a nutsche having an inner diameter of 1/2 was used instead of the nutsche used in Reference Example 1.
- the thickness of the obtained cake was 15 mm, the liquid content of the cake was 38% by weight, and the substitution rate was 95.5%.
- the present invention contributes to the stable operation of the bisphenol A production apparatus, and can efficiently produce high-purity bisphenol A.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2002303001A JP2004137197A (ja) | 2002-10-17 | 2002-10-17 | ビスフェノールaの製造方法 |
JP2002-303001 | 2002-10-17 |
Publications (1)
Publication Number | Publication Date |
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WO2004035512A1 true WO2004035512A1 (ja) | 2004-04-29 |
Family
ID=32105065
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2003/013184 WO2004035512A1 (ja) | 2002-10-17 | 2003-10-15 | ビスフェノールaの製造方法 |
Country Status (5)
Country | Link |
---|---|
JP (1) | JP2004137197A (ja) |
KR (1) | KR101011878B1 (ja) |
CN (1) | CN100406421C (ja) |
TW (1) | TWI318971B (ja) |
WO (1) | WO2004035512A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1541542A1 (en) * | 2002-08-28 | 2005-06-15 | Idemitsu Kosan Co., Ltd. | Process for producing bisphenol a |
EP1982971A4 (en) * | 2006-02-02 | 2011-01-12 | Idemitsu Kosan Co | METHOD AND EQUIPMENT FOR RECOVERING BISPHENOL A |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP5184751B2 (ja) | 2006-03-16 | 2013-04-17 | 出光興産株式会社 | ビスフェノールaの製造方法 |
WO2018225014A1 (en) * | 2017-06-07 | 2018-12-13 | Sabic Global Technologies B.V. | Rotary vacuum filter, method, and use |
WO2020075762A1 (ja) * | 2018-10-09 | 2020-04-16 | 三菱ケミカル株式会社 | (メタ)アクリル酸の精製方法 |
JP2020132612A (ja) * | 2019-02-26 | 2020-08-31 | 三菱ケミカル株式会社 | 固液分離方法、並びに、それを用いた(メタ)アクリル酸の精製方法及び精製(メタ)アクリル酸の製造方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0725798A (ja) * | 1993-07-08 | 1995-01-27 | Idemitsu Petrochem Co Ltd | 高純度ビスフェノールaの製造方法 |
EP0926118A1 (en) * | 1997-12-24 | 1999-06-30 | General Electric Company | Process for the purification of bisphenols and preparation of polycarbonates therefrom |
WO2000015589A1 (en) * | 1998-09-16 | 2000-03-23 | General Electric Company | Liquid vacuum pump seal to reduce contamination in bisphenol-a |
-
2002
- 2002-10-17 JP JP2002303001A patent/JP2004137197A/ja active Pending
-
2003
- 2003-10-15 KR KR1020057006584A patent/KR101011878B1/ko active IP Right Grant
- 2003-10-15 CN CNB2003801015381A patent/CN100406421C/zh not_active Expired - Lifetime
- 2003-10-15 WO PCT/JP2003/013184 patent/WO2004035512A1/ja active Application Filing
- 2003-10-16 TW TW092128733A patent/TWI318971B/zh not_active IP Right Cessation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0725798A (ja) * | 1993-07-08 | 1995-01-27 | Idemitsu Petrochem Co Ltd | 高純度ビスフェノールaの製造方法 |
EP0926118A1 (en) * | 1997-12-24 | 1999-06-30 | General Electric Company | Process for the purification of bisphenols and preparation of polycarbonates therefrom |
WO2000015589A1 (en) * | 1998-09-16 | 2000-03-23 | General Electric Company | Liquid vacuum pump seal to reduce contamination in bisphenol-a |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1541542A1 (en) * | 2002-08-28 | 2005-06-15 | Idemitsu Kosan Co., Ltd. | Process for producing bisphenol a |
EP1541542A4 (en) * | 2002-08-28 | 2006-08-09 | Idemitsu Kosan Co | PROCESS FOR PREPARING BISPHENOL A |
EP1982971A4 (en) * | 2006-02-02 | 2011-01-12 | Idemitsu Kosan Co | METHOD AND EQUIPMENT FOR RECOVERING BISPHENOL A |
Also Published As
Publication number | Publication date |
---|---|
TW200407291A (en) | 2004-05-16 |
TWI318971B (en) | 2010-01-01 |
CN100406421C (zh) | 2008-07-30 |
JP2004137197A (ja) | 2004-05-13 |
KR101011878B1 (ko) | 2011-02-01 |
KR20050053772A (ko) | 2005-06-08 |
CN1705627A (zh) | 2005-12-07 |
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