WO1998052895A1 - Verfahren zur kontinuierlichen herstellung von dihydroxydiarylalkanen - Google Patents
Verfahren zur kontinuierlichen herstellung von dihydroxydiarylalkanen Download PDFInfo
- Publication number
- WO1998052895A1 WO1998052895A1 PCT/EP1998/002643 EP9802643W WO9852895A1 WO 1998052895 A1 WO1998052895 A1 WO 1998052895A1 EP 9802643 W EP9802643 W EP 9802643W WO 9852895 A1 WO9852895 A1 WO 9852895A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- phenol
- bisphenol
- isoalkenylphenol
- reaction
- ketone
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to a process for the continuous preparation of dihydroxydiaiylalkylene (bisphenols) by reacting fresh phenol, phenol and isoalkenylphenol from the cleavage of by-products and of ketone.
- bisphenols dihydroxydiaiylalkylene
- the majority of bisphenol is obtained from the reaction mixture by crystallization, and the mother liquor obtained is freed from phenol by distillation.
- the phenol is fed back into the reaction, and the bottom obtained in the distillation is split in a reactive rectification after addition of a basic catalyst.
- the overhead phenol and isoalkenylphenol are returned to the reaction, the bottom from the 1st reactive column is acidified and further split in the presence of an acidic catalyst in a 2nd reactive rectification into distilling phenol, which is reused in the reaction, and a bottom which is disposed of.
- Alkenylphenols which still have to be thoroughly cleaned, are obtained in moderate yield (US Pat. No. 2,497,503). A hydrogenating treatment also leads to valuable products, as taught by EP-A 17 852. The cleavage can also be accelerated by acidic and basic compounds. With acids such as sulfuric or toluenesulfonic acid, however, only phenol is obtained (US Pat. No. 3,466,337). Basic catalysts, on the other hand, cause the ejected materials to split into phenol and isoalkenylphenol. Alkaline compounds such as NaOH, KOH, NaHCO 3 , Na acetate, Na hypophosphite, K 2 CO 3 , MgO and Al isopropylate (US Pat. No.
- the second mother liquor in the bisphenol process specified above or the first mother liquor after separating the first amount of bisphenol and after the rearrangement be worked up at least partially by distillation in order to make better use of the valuable products contained therein.
- the bisphenol obtained is returned to the first crystallization stage and purified there.
- the low boilers containing isomers are fed to the reaction (WO 94/20445 and EP-A 552 518).
- the difficulty is to obtain from the mother liquor, which is highly enriched in isomers and by-products, with reasonable effort sufficiently pure fractions, which are particularly poor in the difficult-to-remove chromanes and indanes, without increasing the unusable residue too much and reducing the yield . For this reason, some of the distillation products must be discarded.
- the low-bisphenol fractions obtained in the distillation can also be subjected to the cleavage and the cleavage products reintroduced into the process (EP-A 332 203).
- Purity is obtained by a simple, fully continuous process if phenol is reacted with ketone and isoalkenylphenol from the cleavage in such a way that Nig isomers and by-products are formed, unreacted ketone is distilled off, any acidic constituents are separated off, the majority of the bisphenol contained therein is isolated by crystallization, the mother liquor and the washing phenol are combined from this crystallization step, phenol is distilled off and added to the reaction, and the bottoms are added mixed with a basic catalyst and split in a first reactive rectification into overhead phenol and isoalkenylphenol, both of which flow into the reaction, acidifies the bottom obtained in the reactive rectification and in the presence of an acidic catalyst in a second reactive rectification in phenol, which is added to the reaction and cleaves a residue to be disposed of.
- Aromatic hydroxy compounds suitable for the process according to the invention are not substituted in the p-position and contain no second-order substituents such as cyano, carboxy or nitro groups; Examples include phenol, o- and m-cresol, 2,6-dimethylphenol, o-tert-butylphenol, 2-methyl-6-tert-butylphenol, o-cyclohexylphenol, o-phenylphenol, o-isopropylphenol, 2-methyl-6-cyclopentyl-phenol, o- and m-chlorophenol, 2,3,6-trimethylphenol. Phenol, o- and m-cresol, 2,6-dimethylphenol, o-tert-butylphenol and o-phenylphenol are preferred; phenol is particularly preferred.
- Suitable ketones contain at least one aliphatic group on the carbonyl function; Examples include acetone, methyl ethyl ketone, methyl propyl ketone, methyl isopropyl ketone, diethyl ketone, acetophenone, cyclohexanone, cyclopentanone, methyl, dimethyl and trimethylcyclohexanones, which can also have geminal methyl groups such as 3,3-dimethyl-5-methylcyclohexanone (hydroisophorone).
- Acetone, acetophenone, cyclohexanone and their homologs bearing methyl groups are preferred; acetone is particularly preferred.
- Suitable catalysts for the basic cleavage are those mentioned in the literature, preferably alkali oxides and hydroxides, particularly preferably NaOH and KOH. In the process according to the invention, they are incorporated into the melt of the cleavage starting materials worn, dissolved and homogeneously distributed, the temperature expediently between 100 and 200 ° C, preferably 120 and 180 ° C.
- Suitable catalysts for the acid cleavage are those listed in the literature, preferably sulfuric acid, phosphoric acid, phosphorous acid, their partial salts such as NH 4 HSO 4 , NaHSO 4 , KHSO 4 , NaH 2 PO 4 , KH 2 PO 4 , NH 4 H 2 PO 4 , NH 4 H 2 PO 3 , KH 2 P ⁇ 3 and analogues, furthermore the organic derivatives of these acids namely aromatic sulfonic acids and disulfonic acids such as benzene, toluene, xylene, phenolsulfonic acid, diphenyldisulfonic acid, diphenyl ether disulfonic acid, then aromatic phosphonic and phosphinic acids such as Benzene, toluene, xylolphosphonic and phosphinic acid, diphenyl-diphosphonic and diphosphinic acid, also solid acids such as acidic aluminum oxides, clays such as bentonites and mont
- the amounts of catalysts which are added to the mixture to be cleaved are between 0.01% by weight and 5% by weight, preferably 0.05 to 3% by weight, particularly preferably 0.1 to 2% by weight. %, based on the amount of gap mixture.
- the basic catalysts either have to be removed from the bottom after the basic cleavage, which is usually too expensive, or they must first be neutralized by a strong acid before the addition of the required ones Amount of acid catalyst takes place. This ensures that sufficient amounts of active acid are present. Acidification in the sense of the invention thus means that enough acid is added to the bottom of the basic cleavage that both the basic catalyst contained therein is neutralized and, in addition, a sufficient amount of acidic catalyst is available for the subsequent acidic cleavage.
- the catalysts can, for example, be dissolved or suspended in phenol and metered in continuously to the stream flowing in the column. However, it is also possible to add them to the material to be split discontinuously in intermediate containers and then to convey this mixture continuously into the splitting column.
- the columns in which the reactive rectifications are carried out generally correspond to conventional distillation columns. In the columns, a separation by distillation and fractionation of the cleavage products phenol and isoalkenylphenol from the non-cleaved or non-cleavable compounds is superimposed on the cleavage. The fission products go overhead, generally pure enough for their further use. The non-fissile shares are discharged as sump. Reactive rectifications are known to the person skilled in the art and are described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, 5th Ed., Vol. B 4, p. 321-8.
- Preferred procedures for the conversion to bisphenol are those which deliver bisphenol as highly selectively as possible. They are characterized by the fact that one works with the lowest possible ketone concentration. This can be achieved by reacting phenol with ketone and isoalkenylphenol in at least two reactors connected in series, which contain acidic ion exchangers and are operated at as low a temperature as possible, but in the direction of progressive reaction with increasing temperatures, the total amount of ketone and
- Isoalkenylphenol is divided between the individual reactors and homogeneously distributed in the reaction mixture before entering the respective reactors.
- the selectivity for Bisphenol can be increased if the distribution of ketone and isoalkenylphenol is controlled so that the proportion of the total amount per reactor becomes smaller, the higher the temperature of the reactor in question and the reactor cascade within a temperature range of max. 35 to 85 ° C, preferably 38 to 75 ° C, is operated.
- both mixing elements of a known type are expediently attached in order to ensure the homogeneous distribution of ketone and isoalkenylphenol in the starting phenol or reaction mixture, and also heat exchangers for the desired temperature control of the mixture before it passes through the catalyst bed.
- the reaction product After leaving the last reactor of the cascade and separating unreacted ketone, the reaction product is optionally freed from acidic constituents, as described, for example, in US Pat. No. 4,876,391 or EP-A 552 518 and, if appropriate, a fine filtration for separating Catalytic converter and apparatus wear or other solid contamination subjected.
- the reaction mixture then flows into a crystallizer which is customary for bisphenol synthesis and is known to the person skilled in the art (Ullma-in's Encyclopedia of Industrial Chemistry, 5th Ed., Vol. B 2, pp. 3-1 to 3-34; a crystallization process is found e.g. in
- the resulting sump is mixed with a basic catalyst, metered continuously into a reactive rectification and therein at 190 to 270 ° C, preferably 200 to 260 ° C, particularly preferably 210 to 250 ° C and 15 to 0.5 mbar, preferably 12 to 1 mbar, particularly preferably 10 to 1 mbar, split.
- the distillate consisting of phenol and isoalkenylphenol and its oligomers, is fed to the reaction.
- This can optionally be further purified via a column and is added to the reaction stream again. A sump is removed from the bottom of the column and is to be disposed of.
- the water of reaction which is inevitably formed can be removed from the mass balance from the start
- the reaction mixtures leaving the reactor cascade can, before crystallization, 10 to 35% by weight, preferably 12 to 32, particularly preferably 14 to 30
- % By weight contain bisphenol. If the content is unfavorable for crystallization, it can be adjusted by adding or distilling off phenol.
- the process according to the invention has the advantages over the known bisphenol processes of delivering a very pure bisphenol with excellent yield with a significantly simpler and fully continuous procedure.
- BPA was produced according to the following procedure:
- the acetone conversion was 97 to 98%.
- a BPA-phenol adduct was obtained in the usual way by crystallization (C), suction filtration, washing with phenol and pressing (F). After flash distillation of the phenol in vacuo (D), this adduct was 983 parts by weight / h BPA with a purity of 99.78%.
- the mother liquor and washing phenol obtained were continuously evaporated in vacuo (2, 3), the distilled phenol, in part after extraction (E) and separation of water and extractant (6,7), in reaction and laundry returned and the high boiler residue of 425 parts by weight as melt ⁇ , after 0.5% by weight of KOH had been homogeneously distributed therein, was metered into a 20-plate reactive rectification (4) which had a top temperature of 80 to 82 ° C and a bottom temperature of 238 ° C and was operated at 2 mbar. From this reactive column, 376 parts by weight / h of distillate with the composition UI passed, which flowed back into the reaction to BPA. 48 parts by weight / h of residue were discharged from the bottom of the column.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1019997010529A KR20010012573A (ko) | 1997-05-16 | 1998-05-05 | 디히드록시디아릴알칸의 연속적인 제조 방법 |
EP98925534A EP0984913B1 (de) | 1997-05-16 | 1998-05-05 | Verfahren zur kontinuierlichen herstellung von dihydroxydiarylalkanen |
BR9809826-8A BR9809826A (pt) | 1997-05-16 | 1998-05-05 | Processo para a preparação contìnua de dihidroxidiarilalcanos |
US09/423,702 US6307111B1 (en) | 1997-05-16 | 1998-05-05 | Method for continuous production of dihydroxydiarylalkanes |
AU77617/98A AU7761798A (en) | 1997-05-16 | 1998-05-05 | Method for continuous production of dihydroxydiarylalkanes |
JP54987398A JP2001525831A (ja) | 1997-05-16 | 1998-05-05 | ジヒドロキシジアリールアルカン類の連続的な製造方法 |
DE59802737T DE59802737D1 (de) | 1997-05-16 | 1998-05-05 | Verfahren zur kontinuierlichen herstellung von dihydroxydiarylalkanen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19720539A DE19720539A1 (de) | 1997-05-16 | 1997-05-16 | Verfahren zur kontinuierlichen Herstellung von Dihydroxydiarylalkanen |
DE19720539.9 | 1997-05-16 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1998052895A1 true WO1998052895A1 (de) | 1998-11-26 |
Family
ID=7829636
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1998/002643 WO1998052895A1 (de) | 1997-05-16 | 1998-05-05 | Verfahren zur kontinuierlichen herstellung von dihydroxydiarylalkanen |
Country Status (11)
Country | Link |
---|---|
US (1) | US6307111B1 (de) |
EP (1) | EP0984913B1 (de) |
JP (1) | JP2001525831A (de) |
KR (1) | KR20010012573A (de) |
CN (1) | CN1115317C (de) |
AU (1) | AU7761798A (de) |
BR (1) | BR9809826A (de) |
DE (2) | DE19720539A1 (de) |
ES (1) | ES2167900T3 (de) |
TW (1) | TW448148B (de) |
WO (1) | WO1998052895A1 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6133486A (en) * | 1998-12-30 | 2000-10-17 | General Electric Company | Phenol recovery from BPA process waste streams |
JP2003529575A (ja) * | 2000-03-30 | 2003-10-07 | バイエル アクチェンゲゼルシャフト | ビスフェノールaを含む混合物 |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6716729B2 (en) * | 1999-12-22 | 2004-04-06 | Borden Chemical, Inc. | Stable bisphenolic compositions |
US6703530B2 (en) | 2002-02-28 | 2004-03-09 | General Electric Company | Chemical reactor system and process |
CA2527486A1 (en) * | 2002-06-26 | 2004-01-08 | Den Kongelige Veterinaer-Og Landbohojskole | Dual porosity filter |
JP4539012B2 (ja) | 2002-08-08 | 2010-09-08 | 三菱化学株式会社 | フェノールを含むビスフェノールaの精製方法 |
CN102531849A (zh) * | 2005-01-28 | 2012-07-04 | 陶氏环球技术有限责任公司 | 通过使用催化剂在化学反应过程中生产化学产物的方法 |
US7446234B2 (en) * | 2005-09-27 | 2008-11-04 | Council Of Scientific And Industrial Research | Bisphenol compound and process for preparation thereof |
WO2007044139A1 (en) * | 2005-10-07 | 2007-04-19 | Badger Licensing Llc | Bisphenol-a plant yield enhancement |
TWI494296B (zh) | 2011-12-28 | 2015-08-01 | Rohm & Haas | 經處理、促進之離子交換樹脂觸媒之用途 |
TWI494163B (zh) | 2011-12-28 | 2015-08-01 | Rohm & Haas | 經處理、促進之離子交換樹脂觸媒之用途及製造方法 |
KR101812838B1 (ko) * | 2013-07-11 | 2017-12-27 | 주식회사 엘지화학 | 비스페놀a 제조 장치 및 제조 방법 |
CN104817435B (zh) * | 2015-03-31 | 2017-01-11 | 营口市风光化工有限公司 | 一种废料回收制备2,6-二叔丁基苯酚的方法 |
Citations (6)
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US4308404A (en) * | 1977-07-11 | 1981-12-29 | Shell Oil Company | Preparation of bisphenols |
US4391997A (en) * | 1981-10-23 | 1983-07-05 | General Electric Company | Ion exchange catalyzed bisphenol process |
JPS6038335A (ja) * | 1983-08-11 | 1985-02-27 | Mitsui Toatsu Chem Inc | ビスフエノ−ルaの製造方法 |
EP0332203A1 (de) * | 1988-03-11 | 1989-09-13 | MITSUI TOATSU CHEMICALS, Inc. | Verfahren zur Herstellung von hochreinem Bisphenol A |
WO1992009550A1 (en) * | 1990-11-24 | 1992-06-11 | Instytut Ciezkiej Syntezy Organicznej 'blachownia' | A process to obtain high-purity bisphenol a |
JPH05294873A (ja) * | 1992-04-20 | 1993-11-09 | Nippon Steel Chem Co Ltd | ビスフェノールaの製造方法 |
Family Cites Families (24)
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US2497503A (en) | 1946-03-07 | 1950-02-14 | Libbey Owens Ford Glass Co | Preparation of substituted phenols |
US2775620A (en) | 1954-07-12 | 1956-12-25 | Shell Dev | Production of bis (hydroxyaryl) substituted compounds |
US3242219A (en) | 1957-12-31 | 1966-03-22 | Union Carbide Corp | Preparation of bisphenols |
US3466337A (en) | 1967-01-30 | 1969-09-09 | Dow Chemical Co | Regeneration of phenol from bisphenol a and byproducts |
US4209646A (en) | 1974-10-31 | 1980-06-24 | Rhone-Poulenc Industries | Process for crystallizing an adduct of 2,2-di(4-hydroxyphenyl) propane and phenol |
PL103054B1 (pl) | 1976-09-12 | 1979-05-31 | Instytut Ciezkiejsyntezy Organic | Sposob przerobki odpadow z procesu wytwarzania dwufenylolopropanu |
US4308405A (en) | 1978-07-05 | 1981-12-29 | Shell Oil Company | Preparation of bisphenols |
US4258221A (en) | 1979-04-11 | 1981-03-24 | Phillips Petroleum Company | Cleavage of alkylenebisphenols |
US4277628A (en) | 1980-05-20 | 1981-07-07 | General Electric Company | Phenol recovery from bisphenol-A waste streams |
US4400555A (en) * | 1981-10-06 | 1983-08-23 | General Electric Company | Ion exchange catalyzed bisphenol synethesis |
US4594459A (en) | 1985-03-25 | 1986-06-10 | The Dow Chemical Company | Preparation of p-isopropenyl phenol and related compounds |
PL153396B1 (en) | 1987-10-07 | 1991-04-30 | Method of obtaining bisphenol a | |
JPH068260B2 (ja) * | 1988-01-08 | 1994-02-02 | 三井東圧化学株式会社 | ビスフェノールaの製造方法 |
US4859803A (en) | 1988-05-16 | 1989-08-22 | Shell Oil Company | Preparation of bisphenols |
US4876391A (en) | 1988-09-15 | 1989-10-24 | General Electric Company | Process for preparation and purification of bisphenols |
EP0552518B1 (de) | 1992-01-14 | 1995-09-13 | General Electric Company | Verfahren zur Wiedergewinnung von Bisphenol-A aus Ausflusströmen des Herstellungsverfahrens |
US5300702A (en) | 1993-03-01 | 1994-04-05 | Aristech Chemical Corporation | Recovering values from heavy ends in bisphenol-A production |
US5315042A (en) | 1993-03-22 | 1994-05-24 | General Electric Company | Use of partial acetone conversion for capacity increase and quality/yield improvement in the bisphenol-A reaction |
JP2885606B2 (ja) | 1993-05-12 | 1999-04-26 | 出光石油化学株式会社 | 2,2−ビス(4−ヒドロキシフェニル)プロパンの製造方法 |
US5430199A (en) * | 1994-03-28 | 1995-07-04 | General Electric Company | Method for recovering phenol and xanthene values from bisphenol A tars |
US5504251A (en) * | 1995-03-09 | 1996-04-02 | General Electric Company | Co-cracking of BPA and phenol process tars |
US5672774A (en) * | 1995-10-24 | 1997-09-30 | General Electric Company | Phenol tar processing method |
US5783733A (en) * | 1996-06-13 | 1998-07-21 | General Electric Company | Process for manufacture of bisphenol |
RU2120433C1 (ru) * | 1997-02-28 | 1998-10-20 | Дыкман Аркадий Самуилович | Способ переработки фенольной смолы, полученной в производстве фенола и ацетона кумольным методом |
-
1997
- 1997-05-16 DE DE19720539A patent/DE19720539A1/de not_active Withdrawn
-
1998
- 1998-04-17 TW TW087105845A patent/TW448148B/zh active
- 1998-05-05 JP JP54987398A patent/JP2001525831A/ja active Pending
- 1998-05-05 US US09/423,702 patent/US6307111B1/en not_active Expired - Fee Related
- 1998-05-05 KR KR1019997010529A patent/KR20010012573A/ko not_active Application Discontinuation
- 1998-05-05 ES ES98925534T patent/ES2167900T3/es not_active Expired - Lifetime
- 1998-05-05 DE DE59802737T patent/DE59802737D1/de not_active Expired - Fee Related
- 1998-05-05 WO PCT/EP1998/002643 patent/WO1998052895A1/de not_active Application Discontinuation
- 1998-05-05 BR BR9809826-8A patent/BR9809826A/pt not_active IP Right Cessation
- 1998-05-05 CN CN98804930A patent/CN1115317C/zh not_active Expired - Fee Related
- 1998-05-05 EP EP98925534A patent/EP0984913B1/de not_active Expired - Lifetime
- 1998-05-05 AU AU77617/98A patent/AU7761798A/en not_active Abandoned
Patent Citations (6)
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US4308404A (en) * | 1977-07-11 | 1981-12-29 | Shell Oil Company | Preparation of bisphenols |
US4391997A (en) * | 1981-10-23 | 1983-07-05 | General Electric Company | Ion exchange catalyzed bisphenol process |
JPS6038335A (ja) * | 1983-08-11 | 1985-02-27 | Mitsui Toatsu Chem Inc | ビスフエノ−ルaの製造方法 |
EP0332203A1 (de) * | 1988-03-11 | 1989-09-13 | MITSUI TOATSU CHEMICALS, Inc. | Verfahren zur Herstellung von hochreinem Bisphenol A |
WO1992009550A1 (en) * | 1990-11-24 | 1992-06-11 | Instytut Ciezkiej Syntezy Organicznej 'blachownia' | A process to obtain high-purity bisphenol a |
JPH05294873A (ja) * | 1992-04-20 | 1993-11-09 | Nippon Steel Chem Co Ltd | ビスフェノールaの製造方法 |
Non-Patent Citations (2)
Title |
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DATABASE WPI Section Ch Week 9349, Derwent World Patents Index; Class A41, AN 93-392597, XP002075636 * |
PATENT ABSTRACTS OF JAPAN vol. 009, no. 166 (C - 290) 11 July 1985 (1985-07-11) * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6133486A (en) * | 1998-12-30 | 2000-10-17 | General Electric Company | Phenol recovery from BPA process waste streams |
JP2003529575A (ja) * | 2000-03-30 | 2003-10-07 | バイエル アクチェンゲゼルシャフト | ビスフェノールaを含む混合物 |
Also Published As
Publication number | Publication date |
---|---|
KR20010012573A (ko) | 2001-02-15 |
EP0984913A1 (de) | 2000-03-15 |
AU7761798A (en) | 1998-12-11 |
US6307111B1 (en) | 2001-10-23 |
CN1255112A (zh) | 2000-05-31 |
DE59802737D1 (de) | 2002-02-21 |
BR9809826A (pt) | 2000-06-20 |
TW448148B (en) | 2001-08-01 |
DE19720539A1 (de) | 1998-11-19 |
JP2001525831A (ja) | 2001-12-11 |
EP0984913B1 (de) | 2001-11-21 |
CN1115317C (zh) | 2003-07-23 |
ES2167900T3 (es) | 2002-05-16 |
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