WO2005073153A1 - ビスフェノールaのプリルの製造方法 - Google Patents
ビスフェノールaのプリルの製造方法 Download PDFInfo
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- WO2005073153A1 WO2005073153A1 PCT/JP2005/001267 JP2005001267W WO2005073153A1 WO 2005073153 A1 WO2005073153 A1 WO 2005073153A1 JP 2005001267 W JP2005001267 W JP 2005001267W WO 2005073153 A1 WO2005073153 A1 WO 2005073153A1
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- WO
- WIPO (PCT)
- Prior art keywords
- bisphenol
- bpa
- phenol
- nozzle
- melt
- Prior art date
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Classifications
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- 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 process for producing bisphenol A [2,2-bis (4-hydroxyphenyl) propane] (hereinafter sometimes abbreviated as BPA) prill.
- a granulated product of Bisphenol Nore A which can suppress the adhesion of BPA to the bottom of the granulation tower, has a uniform particle size, is rich in fluidity, has a large bulk density, and has a high hardness, that is, bisphenol It relates to a method for efficiently producing A-prils.
- 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 the demand for bisphenol A has been increasing in recent years. It is in.
- This BPA is produced by condensing excess phenol and acetone in the presence of an acidic catalyst and optionally a cocatalyst such as a sulfur compound.
- this BPA has a high melting point of 157 ° C
- the product is usually in the form of granules or flakes, but granules are preferable in consideration of fluidity.
- a granulation step is usually provided to granulate the hot-melt BPA into a particulate product (prill).
- a granulation device such as a spray drier is used, and the BPA is formed into droplets, and then cooled and solidified to perform granulation. If the BPA droplets are large, the cooling effect during cooling and solidification will be reduced, and the temperature of the BPA prill will increase.
- the manufactured BPA prills are shipped in flexible containers, etc. High temperatures create safety issues during transport.
- the temperature of the BPA melt is kept at 200 ° C or less, the liquid depth of the melt at the outlet of the nozzle is 300 mm 2000 mm, and the height of the granulation tower is at least 10,000 mm.
- the range of the speed of the cooling gas that is performed by the method for example, see Patent Document 1.
- the cooling gas velocity Vg should be specified as 0.1 Vp ⁇ Vg ⁇ 0.8 Vp, when the theoretical end drop velocity Vp at the average particle size of BPA prill is Vp. There is no description of the range of the outflow velocity of the melt of BPA, which is proposed (for example, see Patent Document 2).
- ammonium nitrate was used at a liquid height of 75 mm, a hole diameter of 0.75 to 2 mm, a hole interval of 5 to 20 mm, and a cooling gas flow rate of 0.3 to 1.2 m / s.
- a cooling gas flow rate 0.3 to 1.2 m / s.
- Patent Document 1 Japanese Patent Publication No. 47-8060
- Patent Document 2 JP-A-6-107580
- Patent Document 3 Japanese Patent Publication No. 55-22137
- Patent Document 4 Japanese Patent Publication No. 8-4737
- the present invention is stable by defining the pore diameter of the nozzle, the flow rate of the melt of bisphenol A from the nozzle, the flow rate of the cooling gas, and the nozzle hole interval.
- Bisphenol A can be produced, reducing the amount of BPA adhering to the bottom of the granulation tower and out-of-spec products due to it, and eliminating the need for vibration generators and the like in the granulation of BPA. It is an object of the present invention to provide a method for efficiently producing BPA prills having a uniform diameter, high fluidity, high bulk density and high hardness.
- the inventor of the present invention has found that a melt of bisphenol A is dropped from a nozzle plate at the upper part of the granulation tower, and a cooling gas is flowed from the lower part toward the upper part to perform granulation. It has been found that the above object can be achieved by defining the pore size of the melt, the flow rate of the bisphenol A melt from the nozzle, and the flow rate of the cooling gas.
- the present invention has been completed based on strong knowledge.
- bisphenol A is stabilized by defining the pore diameter of the nozzle, the flow rate of the melt of bisphenol A from the nozzle, the flow rate of the cooling gas, and the interval between the nozzle holes.
- the BPA adhesion to the bottom of the granulation tower can be suppressed, the particle size is uniform, the fluidity is high, the bulk density is large, and the strength is high.
- the BPA can be prevented from adhering to the bottom of the granulation tower, long-term operation that requires complicated operation of peeling off the adhering substances by hammering is possible, and economic efficiency is high.
- FIG. 1 is a schematic view showing one example of a granulating apparatus used in the present invention.
- Bisphenol A used in the present invention may be obtained, for example, by (A) a step of condensing an excess of phenol and acetone in the presence of an acidic catalyst to produce bisphenol A, and obtaining a reaction mixture; Condensing the reaction mixture, (C) crystallizing and separating an adduct of bisphenol A and phenol from the concentrated residue obtained in step (B), and (D) performing step (C).
- step (A) of the method for producing bisphenol A excess phenol and acetone are condensed in the presence of an acidic catalyst to produce bisphenol A.
- an acid-type ion exchange resin can be used as the acidic catalyst.
- the acid-type ion-exchange resin those which are conventionally used as a catalyst for bisphenol A can be used, although there is no particular limitation.
- Sulfonic acid-type cation-exchange resin is particularly preferable in terms of catalytic activity and the like. It is suitable.
- 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.
- sulfonic acid type cation exchange resin examples include a sulfone styrene dibutylbenzene copolymer, Cross-linked styrene polymers, phenol formaldehyde sulfonic acid resins, benzene formaldehyde-sulfonic acid resins, and the like.
- mercaptans are usually used in combination with the acid-type ion exchange resin as a co-catalyst.
- the mercaptans refer to compounds having a free SH group in the molecule, such as alkyl mercaptans and alkyl mercaptans having one or more substituents such as carboxyl, amino and hydroxyl groups. , For example, mercaptocarboxylic acid, aminoalkanethiol, mercaptoalcohol and the like.
- Examples of such mercaptans include alkyl mercaptans such as methyl mercaptan, ethyl mercaptan, n-butyl mercaptan, and n-octyl mercaptan; thiocarboxylic acids such as thioglycolic acid and monomercaptopropionic acid; and 2-aminoethanethiol.
- alkyl mercaptans such as methyl mercaptan, ethyl mercaptan, n-butyl mercaptan, and n-octyl mercaptan
- thiocarboxylic acids such as thioglycolic acid and monomercaptopropionic acid
- 2-aminoethanethiol 2-aminoethanethiol.
- aminoalkanethiols such as mercaptoethanol and mercapto alcohols such as mercaptoethanol, etc.
- mercaptans may be used alone or in combination of two or more.
- mercaptans can be immobilized on the above-mentioned acid-type ion-exchange resin and used as promoters.
- the amount of the mercaptan to be used is generally selected in the range of 0.1 to 20% by mole, and preferably in the range of 110 to 10% by mole, based on acetone as a raw material.
- the ratio of phenol to acetone it is desirable that the amount of unreacted acetone be as small as possible from the viewpoint of easy purification and economical efficiency of the produced bisphenol A. Therefore, it is advantageous to use the phenol in excess of the stoichiometric amount.
- the reaction solvent is generally not required, except that the reaction solution is reacted at a low temperature at which the viscosity of the reaction solution is too high or the operation is difficult due to solidification.
- the condensation reaction between phenol and acetone in the above-mentioned production method may be any of a batch type and a continuous type.
- a phenol, an acetone and a mercaptan If the mercaptans are not immobilized on the acid-type ion exchange resin, it is advantageous to use a fixed-bed continuous reaction system in which) is continuously supplied and reacted.
- one or two or more reaction towers may be arranged in series, but industrially, two or more reaction towers filled with an acid-type ion exchange resin are connected in series and fixed. It is particularly advantageous to employ a multi-bed continuous reaction system.
- the acetone / phenol molar ratio is usually selected in the range of 1/30 to 1/3, preferably 1/15 to 1/5.
- 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 / acetone is usually selected in the range of 0.1 / 100-20 / 100, preferably 1 / 100-10 / 100.
- 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 greater than 20Z100, the effect is not much improved depending on the amount. I can't.
- the reaction temperature is generally selected in the range of 40 to 150 ° C, preferably 60 to 110 ° C.
- the reaction rate is slow, and if the viscosity of the reaction solution is extremely high, there is a risk of solidification. If the temperature exceeds 150 ° C., it is difficult to control the reaction.
- the selectivity of ( ⁇ , ⁇ 'integrated) decreases, and the acid type ion exchange resin of the catalyst may decompose or deteriorate.
- the LHSV (liquid hourly space velocity) of the raw material mixture is generally selected in the range of 0.2 to 30 hours—preferably 0.5 to 10 hours— 1 .
- reaction mixture thus obtained is first filtered through a filter.
- Such filtration promotes the decomposition of bisphenol A in the product, and removes catalyst residues and catalyst crushed substances that deteriorate the hue.
- an adduct of bisphenol A and phenol is added using a phenol-containing solution together with the following step (B) and step (F). At least one of a step of dissolving and a step of crystallizing and separating the adduct from the solution is performed by a filtration step using a filter.
- the step (B) is a step of concentrating the reaction mixture substantially containing no acid-type ion exchange resin.
- concentration step generally, first, unreacted acetone, by-product water, and low-boiling substances such as alkylmercaptan are removed by reduced-pressure distillation using a distillation column. 6. carried out at 5 80 kPa approximately, and temperature 70 180 ° C about conditions.
- the temperature of the heating source used is desirably 190 ° C or lower in order to prevent the thermal decomposition of bisphenol A.
- the bottom liquid containing bisphenol A and phenol, etc., from which the low-boiling substances have been removed from the reaction mixture is subjected to vacuum distillation to remove phenol, and to concentrate bisphenol A.
- conditions of normal temperature of about 100 to 170 ° C and pressure of about 5 to 70 kPa are adopted.
- this temperature is lower than 100 ° C, high vacuum is required, and if it is higher than 170 ° C, extra heat removal is required in the next crystallization step, which is not preferable.
- the concentration of bisphenol A in the concentrated residue is preferably in the range of 20 to 50% by mass, and more preferably 20 to 40% by mass.
- the concentration is less than 20% by mass, the recovery of bisphenol A is low. If it exceeds 50% by mass, it may be difficult to transfer the slurry after crystallization.
- a 1: 1 adduct of bisphenol A and phenol (hereinafter sometimes referred to as phenol adduct) is crystallized and separated from the concentrated residual liquid obtained in the above step (B). It is a process to do.
- the concentrated residue is cooled to about 40 to 70 ° C., and the phenol adduct is crystallized to form a slurry.
- the cooling at this time may be performed using an external heat exchanger, or may be performed by a vacuum cooling crystallization method in which water is added to the concentrated residual liquid and cooling is performed using latent heat of evaporation of water under reduced pressure.
- a vacuum cooling crystallization method in which water is added to the concentrated residual liquid and cooling is performed using latent heat of evaporation of water under reduced pressure.
- the amount of water is less than 3% by mass, the heat removal ability is not sufficient. If it exceeds 20% by mass, 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 or solidify. If the crystallization temperature exceeds 70 ° C, the dissolution loss of bisphenol A increases, which is preferable. Absent.
- the slurry containing the phenol adduct thus crystallized is filtered or centrifuged.
- the solution is separated into the outside of the phenol and the crystallization mother liquor containing a reaction by-product.
- the step (D) is a step of dissolving the phenol adduct crystallized and separated in the step (C) using a phenol-containing solution.
- the phenol-containing solution used in this step is not particularly limited.
- the recovered phenol obtained in the concentration step of the above (B) step, the washing liquid of the phenol adduct generated in the crystallization and separation step of the step (C), The mother liquor in the solid-liquid separation of the crystallized phenol adduct and the washing liquid of the phenol adduct generated in the steps after the step (D) can be mentioned.
- the above-mentioned phenol-containing solution is added to the phenol adduct obtained in the step (C), heated to about 80110 ° C, and the phenol adduct is dissolved by heating.
- the bisphenol A-containing solution prepared in this way is relatively low in viscosity and has a low viscosity even at temperature, and is relatively easy to handle.
- the solid-liquid separation of the phenol adduct crystallized in the next step is performed by a filter. Suitable for
- this step the outside of phenol aladder is crystallized and separated from the bisphenol A-containing solution obtained in the above step (D), and in some cases, in order to obtain a high-purity product, the phenol aduct is further added to the phenol-containing solution.
- This is a step of repeating the operation of dissolving with crystallization and then crystallization and separation at least once.
- the step (F) is a step of heating and melting the phenol adduct crystallized and separated in the step (E), and then distilling off the phenol.
- the vacuum distillation is generally carried out under the conditions of a pressure of 11 lkPa and a temperature of 150 to 190 ° C.
- Residual phenol can be further removed by steam stripping or nitrogen stripping.
- the granulation tower is a device in which a nozzle plate in which a BPA melt is dropped is installed at the top, and a duct for blowing a cooling gas is provided at the bottom of the tower.
- a metal plate or the like provided with a large number of holes is used as the nose plate, and can be heated by an electric heater, steam, or the like in order to prevent the BPA from sticking.
- the tower height is determined by the cooling time of the BPA droplet, but is usually about 10-50 m.
- the granulating device for example, the one shown in FIG. 1 can be used.
- the BPA melt purified in the step (F) flows out of the granulation nozzle 1 to become BPA droplets, and falls in the granulation tower 2 in a shower shape.
- the BPA droplets are cooled by the gas introduced from the cooling gas inlet 3 into BPA prills, and the BPA prills are discharged from the granulation delivery port 4.
- the gas used for cooling is discharged from the gas outlet 5.
- the temperature of the BPA melt is preferably 157-200 ° C.
- the temperature is 157-180 ° C.
- the temperature of the BPA melt is lower than 157 ° C, it may be solidified, and if it exceeds 200 ° C, it may be colored.
- the granulation nozzle 1 has a plate provided with a lip.
- the pore diameter (diameter) of the horn is 0.3-1. Omm, preferably 0.4-0.7 mm, more preferably 0.5-0.6 mm, so that the average particle size is 0.5-1.5 BPA prills of about 5mm can be obtained.
- the outflow velocity of the BPA melt discharged from the granulation nozzle 1 needs to be 0.5-1.8 m / s, preferably 1.0-1.8 m / s, more preferably Is 1.4-1.8 m / s. If the outflow velocity of the BPA melt is 0.5 m / s or more, the BPA droplets will not coalesce and become large, and if the outflow velocity of the BPA melt is 1.8 m / s or less, the BPA liquid The droplets do not coalesce and their size is uniform.
- the BPA melt reaches the bottom of the granulation tower with the BPA melt remaining and adheres to the bottom.
- the outflow speed of the BPA melt can be adjusted by adjusting the flow rate of the BPA melt to the nozzle.
- the distance between the holes of the nozzle of the present invention is 5 to 12 mm, preferably 7 lmm, and more preferably 810 mm.
- hole interval refers to the distance between the centers of adjacent holes.
- the distance between the holes is more than 12 mm, the distance between the BPA droplets increases, so that it is difficult for the droplets to coalesce even if the BPA melt flows out slightly from the nozzle.
- the number of nozzles increases, the number of nozzle plates increases, and the diameter of the granulation tower must be increased.
- the number of nozzle plates is appropriate, and it is not necessary to increase the diameter of the granulation tower.
- the BPA melt flows unevenly, and the force S that may cause the droplets that have flowed obliquely to coalesce S. If the distance between the nozzle holes is 5 mm or more, the uneven flow is more likely. Even after this, coalescence of the droplets of BPA becomes difficult to occur.
- inert nitrogen is used because BPA has a property of being easily oxidized.
- the gas flow rate in the granulation tower 2 is 0.7-2.
- OmZs preferably 0.9-1.8 mZs, more preferably 1.0-1.6 mZs.
- the temperature inside the granulation tower 2 can be kept at 40-90 ° C, and the temperature of the BPA prill should be cooled to 50-60 ° C. Can be.
- the velocity of the cooling gas is 0.7 m / s or more, the cooling of the BPA melt is appropriate.On the other hand, when the velocity is 2.0 Om / s or less, the BPA particles fall easily, Collision does not occur, reducing the production of BPA fines and increasing the yield of BPA prills.
- SUS304, SUS316, SUS316L, and the like are generally used as materials for equipment from the step (A) to the granulation tower.
- Acetone, water, ethyl mercaptan, etc. were removed from the resulting reaction mixture by vacuum distillation at a tower bottom temperature of 170 ° C and a pressure of 67 kPa, followed by vacuum distillation at a temperature of 130 ° C and a pressure of 14 kPa. Then, the phenol was distilled off, and the mixture was concentrated until the bisphenol A concentration became 40% by mass to obtain a phenol'bisphenol A solution.
- the Adakuto added phenol to, to prepare a solution containing phenol 60 mass 0/0 and Bisufue Nord eight 40 wt% was heated to 90 ° C.
- the adduct crystal was heated and melted at 130 ° C., and then dephenol was removed to obtain bisphenol A.
- Nitrogen gas at 40 ° C was supplied from the bottom of the granulation tower with a tower diameter of 2.2 m and a tower height of 30 m so that the gas velocity was 1.6 m / s.
- this granulation tower there is a nozore plate with holes of 0.5 mm in diameter opened at 9 mm intervals.
- a bisphenol A melt at a temperature of 170 ° C was supplied to this plate at an outflow rate of 1.4 mZs to granulate BPA.
- BPA prills with an average particle size of 1. Omm could be produced stably for 2 weeks.
- the gas velocity of nitrogen gas at 40 ° C was 1.Om/s
- the outflow velocity of bisphenol A melt at a temperature of 170 ° C was 1.8m. / s, and granulated BPA.
- BPA prills with an average particle size of 1.1 mm could be produced stably for two weeks.
- a nose plate with holes having a diameter of 0.6 mm was formed at intervals of 5 mm.
- the BPA was granulated by supplying a nitrogen gas at 40 ° C at a gas velocity of 1.6 m / s and a bisphenol A melt at 170 ° C at a flow rate of 1.5 m / s.
- a nitrogen gas at 40 ° C at a gas velocity of 1.6 m / s
- a bisphenol A melt at 170 ° C at a flow rate of 1.5 m / s.
- BPA prills with an average particle size of 1.1 mm could be produced stably for two weeks.
- Example 2 At the top of the same granulation tower as in Example 1, a nozore plate having holes with a diameter of 0.5 mm opened at intervals of 5 mm was installed.
- the BPA was granulated by supplying a nitrogen gas at 40 ° C at a gas velocity of 1.lm / s and a bisphenol A melt at 170 ° C at a flow rate of 1.8m / s.
- a nitrogen gas at 40 ° C at a gas velocity of 1.lm / s and a bisphenol A melt at 170 ° C at a flow rate of 1.8m / s.
- BPA prills with an average particle size of 1.1 mm could be produced stably for two weeks.
- Example 4 In the same granulating tower as in Example 4 (nozzle plate with holes of 0.5 mm in diameter and drilled at 5 mm intervals), the gas velocity of nitrogen gas at 40 ° C was set to 1. lmZs and temperature at 170 ° C. BPA was granulated by feeding the bisphenol A melt at a flow rate of 2.9 m / s. As a result, BPA prills with an average particle size of 1.6 mm could be produced stably for two weeks.However, when the granulation tower was inspected two weeks later, BPA was attached to the bottom of the tower at a thickness of about 10 mm. I was
- Table 1 shows the test results.
- Example 2 In the same granulation tower as in Example 1 (nozzle plate with holes of 0.5 mm in diameter and holes of 9 mm) was installed, the gas velocity of nitrogen gas at 40 ° C was 0.5 m / s, and the temperature was 170 °.
- the bisphenol A of C was fed at a melt flow rate of 1.8 mZs to granulate BPA.
- BPA prills with an average particle diameter of 1.3 mm were able to be produced stably over a period of two weeks.However, when the granulation tower was inspected two weeks later, BPA was attached to the bottom of the tower at a thickness of about 50 mm. I was
- Comparative Example 3 In the same granulation tower as in Example 1 (nozzle plate with holes of 0.5 mm in diameter and holes at 9 mm intervals), the gas velocity of nitrogen gas at 40 ° C was 1.6 m / s, and the temperature was 170 °. The bisphenol A of C was fed at a melt flow rate of 0.4 m / s to granulate BPA. As a result, the droplets of the BPA melt coalesce, have a large particle size, fall without being completely solidified, collide with the bottom of the granulation tower, adhere and accumulate, and eventually the granulation tower becomes blocked. Oops.
- Table 1 shows the test results.
- Example 3 In the same granulation tower as in Example 3 (nozzle plate with holes of 0.6 mm in diameter and drilled at 5 mm intervals), the gas velocity of nitrogen gas at 40 ° C was 2.5 mZs, and the temperature was 170 mC. BPA was granulated by feeding the bisphenol A melt at a flow rate of 1.5 mZs. As a result, BPA prills with an average particle size of 1.2 mm could be produced stably for two weeks, but BPA fines in the nitrogen gas outlet increased.
- Table 1 shows the test results.
- Example 2 In the same granulation tower as in Example 1 (nozzle plate with holes of 0.5 mm in diameter and holes of 3 mm were installed), the gas velocity of nitrogen gas at 40 ° C was set to 1. Om / s and the temperature was set to 170 °. BPA was granulated by feeding the bisphenol A melt at a rate of 1.8 m / s. As a result, BPA prills with an average particle size of 1.6 mm could be produced stably for 2 weeks.However, when the granulation tower was inspected after 2 weeks, BPA was found to adhere to the bottom of the tower at a thickness of about 30 mm. I was
- Table 1 shows the test results.
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Abstract
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KR1020067015227A KR101050655B1 (ko) | 2004-01-29 | 2005-01-28 | 비스페놀 a의 프릴의 제조방법 |
CN2005800032919A CN1914141B (zh) | 2004-01-29 | 2005-01-28 | 制备双酚a球粒的方法 |
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JP2004-021215 | 2004-01-29 | ||
JP2004021215A JP4590188B2 (ja) | 2004-01-29 | 2004-01-29 | ビスフェノールaのプリルの製造方法 |
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JP (1) | JP4590188B2 (ja) |
KR (1) | KR101050655B1 (ja) |
CN (1) | CN1914141B (ja) |
RU (1) | RU2370309C2 (ja) |
TW (1) | TW200530169A (ja) |
WO (1) | WO2005073153A1 (ja) |
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JP2010155803A (ja) * | 2008-12-26 | 2010-07-15 | Mitsubishi Chemicals Corp | ビスフェノール化合物粒子の製造方法 |
KR102588709B1 (ko) * | 2019-03-26 | 2023-10-13 | 주식회사 엘지화학 | 프릴타워 스팀공급량 제어시스템 및 이의 제어방법 |
Citations (1)
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JPH06107580A (ja) * | 1992-09-30 | 1994-04-19 | Nippon Steel Chem Co Ltd | ビスフェノールaプリルの製造方法 |
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- 2005-01-28 KR KR1020067015227A patent/KR101050655B1/ko active IP Right Grant
- 2005-01-28 RU RU2006130969/15A patent/RU2370309C2/ru active
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JPH06107580A (ja) * | 1992-09-30 | 1994-04-19 | Nippon Steel Chem Co Ltd | ビスフェノールaプリルの製造方法 |
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JP2005213190A (ja) | 2005-08-11 |
CN1914141A (zh) | 2007-02-14 |
RU2370309C2 (ru) | 2009-10-20 |
CN1914141B (zh) | 2010-06-16 |
TW200530169A (en) | 2005-09-16 |
KR20060132880A (ko) | 2006-12-22 |
RU2006130969A (ru) | 2008-03-10 |
TWI351397B (ja) | 2011-11-01 |
KR101050655B1 (ko) | 2011-07-19 |
JP4590188B2 (ja) | 2010-12-01 |
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