WO2007086223A1 - ビスフェノールaプリルの製造方法 - Google Patents
ビスフェノールaプリルの製造方法 Download PDFInfo
- Publication number
- WO2007086223A1 WO2007086223A1 PCT/JP2006/325843 JP2006325843W WO2007086223A1 WO 2007086223 A1 WO2007086223 A1 WO 2007086223A1 JP 2006325843 W JP2006325843 W JP 2006325843W WO 2007086223 A1 WO2007086223 A1 WO 2007086223A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- bisphenol
- circulating gas
- phenol
- prill
- gas
- Prior art date
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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
-
- 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
-
- 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
- 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
- C07C37/685—Processes comprising at least two steps in series
-
- 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
- C07C37/74—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- 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
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/86—Purification; separation; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification
Definitions
- the present invention relates to a method for producing a molten bisphenol A prill or other bisphenol A prill, and more particularly to a method for producing a high-quality bisphenol A prill stably and continuously for a long period of time. .
- Bisphenol A is often used as a raw material for polycarbonate resin, which has been increasingly demanded as an engineering plastic in recent years, and its handling ability is mainly distributed as a particulate solid called prill.
- the equipment for granulating this prill is generally a granulation tower equipped with a nozzle for spraying bisphenol A melt at the top of the tower, and a circulation extracted from the top of the granulation tower.
- Heat exchange equipment for cooling the gas, blower for circulating and supplying the cooling gas, and top of the granulation tower To remove and recover the bisphenol A powder entrained in the extracted circulating gas It consists of powder removal equipment.
- Spray towers and heat exchangers are used as heat exchange equipment for cooling this circulating gas.
- the components of the cleaning liquid are mixed into the circulating gas, which adversely affects the quality of the product bisphenol A.
- the water content of bisphenol A increases.
- the increased water content of bisphenol A degrades the fluidity and makes it difficult to handle.
- Patent Document 2 a method of producing bisphenol A prill by dropping a melt of bisphenol A also with the force of the upper part of the granulation tower and flowing a cooling gas upward from the bottom, cooling and solidifying the liquid droplets.
- a heat exchanger (cooler) is used as a heat exchange facility for cooling the circulating gas, and the circulating gas temperature at the outlet of the granulation tower is controlled to 60 to 80 ° C. For the concentration of phenol, let's talk about it.
- the deposit on the bottom of the granulation tower becomes a colored scale with a high impurity concentration. If it is sequestered for some reason, it is discharged together with bisnofeal A prill, which may cause product quality problems.
- Patent Document 1 Japanese Translation of Special Publication 2002-534402
- Patent Document 2 JP-A-6-107581
- the object of the present invention is to reduce the heat transfer due to the formation of deposits in the heat exchanger in the granulation process when producing bisphenol A prill from molten bisphenol A,
- the purpose is to provide a method for producing high-quality bisphenol A prills stably and continuously for a long period of time, eliminating the increase in differential pressure.
- the present inventors have found that the molten bisphenol A obtained in the adduct decomposition process has a high molecular weight, such as a molten droplet surface force, when it becomes a prill. Lyabisphenol A and isopropylphenol are released, and this gas accumulates in the granulation tower. , Circulating gas cooler tubes and fins table On the surface, the cyclic dimer generated from bisphenol A or isopropanol phenol is prevented from adhering to phenol as a binder, and in the granulation process, the concentration of phenol in the circulating gas is controlled to ensure high quality.
- the inventors have found that bisphenol A prill can be stably produced continuously for a long period of time, and the present invention has been achieved.
- the present invention provides the following method for producing bisphenol A prill.
- a granulation tower that granulates by spraying molten bisphenol A and bringing it into contact with the circulating gas, powder removal equipment that removes bisphenol A powder in the circulating gas, and circulating gas cooling to adjust the circulating gas temperature
- the phenol concentration in the circulating gas should be controlled to 50 ppm by volume or less.
- FIG. 1 is an explanatory view showing an example of the flow of a granulating apparatus in the method for producing bisphenol A prill of the present invention.
- FIG. 2 is an explanatory diagram showing the structure of a vertical heat transfer multitubular heat exchanger (with fins) used in a circulating gas cooler.
- the condensation reaction step is a step of subjecting phenol and acetone to a condensation reaction in the presence of an acidic catalyst.
- the raw materials phenol and acetone are reacted in a stoichiometric excess of phenol.
- the phenol / acetone molar ratio is usually in the range of 3-30, preferably 5-20.
- the reaction temperature is usually 50 to 100 ° C.
- the reaction pressure is usually normal pressure to 1.5 MPa, preferably normal pressure to 0.6 MPa.
- a sulfonic acid type strongly acidic cation exchange resin is usually used.
- a catalyst obtained by neutralizing a part of the strong acid cation exchange resin catalyst with a promoter such as mercaptoalkylamine may be used.
- the condensation reaction between phenol and acetone is carried out by a continuous method and a fixed bed flow method which is a forced flow method or a suspension bed batch method.
- a fixed bed flow method the liquid space velocity of the raw material liquid supplied to the reactor is about 0.2 to 50 hr- 1 .
- the amount of the resin catalyst is generally in the range of 20 to 100% by mass with respect to the raw material liquid, and the treatment time is 0.5 to 5 hours.
- the concentration step is a step of concentrating the reaction mixture obtained in the condensation reaction step.
- the reaction mixture from the condensation reaction step is usually concentrated in two steps.
- unreacted acetone, reaction product water, and the like are removed by a method such as vacuum distillation. Distillation under reduced pressure is usually carried out at a temperature of 30 to 180 ° C and a pressure of 13 to 67 kPa.
- the second dark In the shrinking process phenol is distilled off and the concentration of bisphenol A is adjusted.
- the concentration of bisphenol A in this case preferably be 20 to 60 mass 0/0! /,.
- the concentration is usually adjusted by pre-concentrating the reaction mixture in the first concentration step.
- This second concentration step is usually preferably carried out under conditions of a pressure of 4 to 40 kPa and a temperature of 70 to 140 ° C.
- the crystallization and solid-liquid separation step is a step of cooling the concentrated liquid obtained in the concentration step to crystallize an adduct of bisphenol A and phenol and separating it into the adduct and the mother liquor.
- the concentrated solution from the concentration step is usually cooled from 70 to 140 ° C to 35 to 60 ° C, and an adduct of bisphenol A and phenol is crystallized into a slurry. Cooling is performed by external heat exchange or heat removal by evaporation of water added to the crystallizer.
- the slurry liquid is solid-liquid separated. Since the mother liquor obtained in the crystallization / solid-liquid separation step contains reaction product water, it is usually introduced into a dehydration tower. However, a part of the hydrated mother liquor may be circulated to the crystallizer.
- the composition of the mother liquor after dehydration is usually: phenol: 65 to 85% by mass, bisphenol A: 10 to 20% by mass, 2,4 'by-products such as isomers: 5 to 15% by mass, 2, 4' It contains many impurities such as isomers.
- This mother liquor is usually treated in an isomerization treatment step, and the phenol and bisphenol A contained in the mother liquor are recovered.
- the adduct recovered by the solid-liquid separation is then sent to an adduct decomposition process to remove phenol to obtain high-purity bisphenol A.
- the solid component mainly composed of adducts filtered and deposited on the filter surface of the solid-liquid separator is subjected to washing with the washing liquid.
- the cleaning liquid used is the same as the saturated phenol solution of bisphenol A, in addition to the recovered phenol by evaporation, raw material phenol, water, water-phenol mixture.
- the amount of cleaning solution used is large. Force is naturally good in terms of cleaning efficiency. There is an upper limit naturally from the viewpoint of loss of crystal re-dissolution, circulation, recovery and reuse of cleaning solution. The most effective amount is about 0.1 to 10 times the amount of crystals.
- the crystal may be redissolved, and the crystallization and solid-liquid separation may be repeated again.
- This crystal By repeating prayer and solid-liquid separation in multiple stages, the impurities incorporated in the adduct crystal are reduced in sequence.
- the re-dissolved solution and the solid component cleaning solution mainly composed of an adduct obtained by solid-liquid separation include phenol collected by evaporation, raw material phenol, water, water-phenol mixture, The same bisphenol A saturated phenol solution can be used at each stage.
- the mother liquor obtained by recrystallization and solid-liquid separation can be recycled to the previous crystallization process.
- the solid-liquid separation device used for solid-liquid separation is not particularly limited as long as it is usually used, but a belt filter, a drum filter, a tray filter, a centrifugal separator and the like are used.
- the adduct decomposition process is a process of removing bisphenol A from the adduct of bisphenol A and phenol and recovering bisphenol A.
- the adduct recovered by the solid-liquid separation can be obtained by removing phenol in the adduct decomposition process to obtain high purity bisphenol A.
- the adduct is heated and melted at about 100 to 160 ° C. to decompose into bisphenol A and phenol, and most of the phenol is removed by this molten liquid evaporator. By removing the remaining phenol by steam stripping, a melt of bisphenol A is obtained.
- the granulation process is a process in which the molten bisphenol A obtained in the adduct decomposition process is granulated to separate the product bisphenol A.
- Fig. 1 shows an example of the flow of the granulating apparatus in the method for producing bisphenol A prill of the present invention.
- Fig. 1 the melt of bisphenol A obtained by the decomposition of adduct is fed from the flow path 1 to the top of the granulating tower 3, and the nozzle provided in the nozzle plate chamber 1 installed at the top of the tower. Sprayed from multiple holes in plate 10.
- the sprayed molten liquid is cooled by the circulating gas 4 rising from the bottom of the granulating tower 3, and is extracted from the flow path 9 as a particulate solid called prill from the bottom of the tower to become bisphenol A prill.
- Tower top force Outflowing circulating gas 4 is accompanied by bisphenol A powder.
- the accompanying powder is collected and collected by a powder removal equipment 5 such as a bag filter.
- the recovered powder may be taken out of the system via the channel 6 or may be directly melted and returned to the bisphenol A production process.
- the circulating gas from which the powder has been removed is increased in pressure by the blower 7 and adjusted in temperature by the circulating gas cooler 8 and then introduced from the bottom of the granulation tower for circulation. Next, each equipment of a granulation process is demonstrated.
- the molten bisphenol A from the adduct decomposition process passes through the orifice and strainer in the nozzle plate chamber and is supplied to the nozzle plate.
- the nozzle plate has a hole diameter of 0.3 to 1. Omm, a flow rate of molten bisphenol A from the nozzle of 0.5 to 1.8 mZs, and a circulating gas flow rate of 0.7 to 2 OmZs. It is preferable. Moreover, it is preferable that the hole interval of a nozzle plate is 5-12 mm.
- the nozzle plate installed at the top of the tower is installed in a deep position in the granulation tower so that the spray in the nozzle holes is not directly affected by the flow of the circulating gas.
- a plurality of spray plates are installed at the top of the granulation tower, and the outermost spray plate has a bisphenol A droplet sprayed from the spray plate so that it does not adhere to the inner wall of the granulation tower. It is preferable to keep the holding distance from the inner wall of the granulation tower.
- the plurality of nozzle plates be evenly installed (for example, arranged in two rows or around the circumference) within a range where the holding distance satisfying the above conditions is taken from the inner wall of the granulation tower.
- This ensures uniform heat exchange between the molten bisphenol A sprayed from the nozzle plate and the circulating gas, reducing the possibility of adhering to the tower bottom as a molten liquid without solidifying the tower bottom.
- a uniform circulation gas flow can be created by providing an evenly divided opening at the bottom of the granulation tower as a circulation gas inlet and installing a rectifying plate that can be removed. it can.
- the inner surface of the cone at the bottom of the tower should be finished with puff 200 or more and a knocker placed on the wall of the bottom of the tower. I like it.
- a typical example of the powder removal equipment is a bag filter.
- Bisphenol A powder is a material that is very adherent and easy to assemble bridges. Therefore, not only is a knocker placed on the wall surface of the bag filter, but a puff finish (200 or more) is applied to the inner surface to prevent bridging. As a countermeasure, it is desirable to install a blaster that discharges a large amount of inert gas at once.
- an inert gas such as nitrogen gas is generally used to remove and collect the bisphenol A powder adhering to the bag filter.
- the amount of inert gas supplied is insufficient for the inert gas used in the bag filter.
- the inert gas used in the bag filter is used. Apart from this, it is necessary to supply new inert gas into the granulation system.
- the general heat exchange ⁇ used to cool the gas is used, and it is preferable to install a multi-tube heat exchange with fins attached to a circular pipe.
- the circulating gas cooler is a vertical heat transfer multi-tube heat exchanger (with fins), and the heat transfer tube bundle can be easily attached and removed on site such as lifting the heat transfer tube bundle with a crane. It is preferable.
- reference numeral 11 is a heat exchanger tube bundle lifting crane
- 12 is a heat exchanger tube bundle lifting hook
- 13 is a multi-tube heat exchanger (with fins) tube bundle
- 14 is a circulating gas flow path
- 15 is A cooling water flow path 16 is a heat exchanger outer shell (casing).
- Deposits adhering to the extracted tubes and fins of the heat exchanger can be removed by washing with a solvent (for example, acetone or phenol).
- a solvent for example, acetone or phenol.
- an inert gas can be used as the circulating gas.
- nitrogen gas is generally used.
- the phenol concentration in the circulating gas in the granulation step is controlled to 50 ppm by volume or less, and preferably 30 ppm by volume or less.
- the volume is controlled to 50 ppm or less, adhesion of bisphenol A powder and impurities to the inside of the circulating gas cooler and granulation tower can be avoided, and the amount of circulating gas can be reduced for a long time without causing a decrease in the circulating gas system's differential pressure.
- the phenol concentration in the circulating gas can be measured with a portable gas detector (for example, a Kitagawa gas detector).
- a portable gas detector for example, a Kitagawa gas detector.
- the method (1) it is preferable to supply a new inert gas of 60 Nm 3 or more per ton of molten bisphenol A supplied to the granulator into the granulation system.
- the position after supplying or returning the gas or inert gas after adsorption or washing of phenol into the granulation system and a part of the circulating gas are extracted.
- the position is not particularly limited, for example, in FIG. 1, the gas after adsorption or cleaning is introduced into the suction line of the blower and the inert gas is introduced into the suction line of the circulating gas cooler. If a part is extracted, the method (1) has less impact on the environment, and the methods (2) and (3) are advantageous for adsorption and washing, and a blower is not required for this purpose.
- a sprinkling tower or a packed tower is used as the gas cleaning device in the method (3), and it is desirable to dry with a dehydrating agent or heat after the gas cleaning.
- molten bisphenol A solution lOtZh is fed to the top of the granulation tower, and the circulating gas is pressurized with a blower (discharge pressure 3kPa-G), and the circulating gas (70, 00 0Nm 3 / h) was supplied to obtain a prill.
- a blower discharge pressure 3kPa-G
- the circulating gas 70, 00 0Nm 3 / h
- the circulating gas cooler inlet temperature was 67-68 ° C throughout the year, and the circulating gas heat exchanger outlet temperature was able to operate at the target of 40 ° C.
- the increase in the differential pressure in heat exchange ⁇ is as small as about 5 kPa, and the decrease in heat removal capacity due to the decrease in air volume due to this and the decrease in overall heat transfer coefficient due to the deposits on the fins I could not see it and was able to drive stably.
- a pale yellow scale was discharged about 0. OlkgZ days.
- 700Nm 3 Zh nitrogen gas 70Nm 3 Zt—molten bisphenol A
- 70Nm 3 Zt—molten bisphenol A is supplied to the granulation tower, and the same amount is withdrawn outside the system to maintain a slight pressure (lkPa-G).
- the phenol concentration was controlled at 20-50 ppm by volume.
- the chilled water tower was controlled so that the temperature of the chilled water to the circulating gas cooler (transmission surface 3,000m 2 , finned multi-tube heat exchanger) was 20 ° C to 35 ° C.
- the circulating gas cooler inlet temperature was 67-68 ° C throughout the year, and the circulating gas heat exchanger outlet temperature was able to operate at the target of 40 ° C.
- the increase in the differential pressure in the heat exchanger is as small as 8 kPa.
- the heat removal capability did not decrease due to a decrease in the overall heat transfer coefficient due to deposits on the tank, and stable operation was possible.
- a pale yellow colored scale was discharged about 0.02 kgZ days.
- the heat transfer is reduced due to the formation of deposits in the heat exchanger in the granulation process, and the differential pressure is increased. This eliminates the possibility of producing high-quality bisphenol A prills stably and continuously for a long period of time.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP06843227A EP1978011A4 (en) | 2006-01-27 | 2006-12-26 | PROCESS FOR PREPARING BISPHENOL-A-PRILL |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2006-019790 | 2006-01-27 | ||
JP2006019790A JP2007197391A (ja) | 2006-01-27 | 2006-01-27 | ビスフェノールaプリルの製造方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2007086223A1 true WO2007086223A1 (ja) | 2007-08-02 |
Family
ID=38309024
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2006/325843 WO2007086223A1 (ja) | 2006-01-27 | 2006-12-26 | ビスフェノールaプリルの製造方法 |
Country Status (7)
Country | Link |
---|---|
EP (1) | EP1978011A4 (ja) |
JP (1) | JP2007197391A (ja) |
KR (1) | KR20080090455A (ja) |
CN (1) | CN101336221A (ja) |
RU (1) | RU2008134904A (ja) |
TW (1) | TW200728265A (ja) |
WO (1) | WO2007086223A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103275335A (zh) * | 2013-05-20 | 2013-09-04 | 安徽理工大学 | 一种聚乙烯蜡微粉的制备方法及喷雾造粒系统 |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4952018B2 (ja) * | 2006-03-29 | 2012-06-13 | 三菱化学株式会社 | 粒状ビスフェノールaの製造方法 |
JP2011213641A (ja) * | 2010-03-31 | 2011-10-27 | Mitsubishi Chemicals Corp | ビスフェノールa製造装置の洗浄方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH06107581A (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 |
JPH09194414A (ja) * | 1996-01-11 | 1997-07-29 | Mitsubishi Chem Corp | ビスフェノールaの製造方法 |
JP2002534402A (ja) | 1999-01-07 | 2002-10-15 | バイエル アクチェンゲゼルシャフト | ビスフェノールaプリルの製造方法及び製造装置、並びにそれに従って製造されるビスフェノールaプリル |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP3686682B2 (ja) * | 1992-09-30 | 2005-08-24 | 新日鐵化学株式会社 | ビスフェノールaの製造方法 |
-
2006
- 2006-01-27 JP JP2006019790A patent/JP2007197391A/ja not_active Withdrawn
- 2006-12-26 RU RU2008134904/04A patent/RU2008134904A/ru not_active Application Discontinuation
- 2006-12-26 CN CNA2006800519407A patent/CN101336221A/zh active Pending
- 2006-12-26 KR KR1020087018112A patent/KR20080090455A/ko not_active Application Discontinuation
- 2006-12-26 WO PCT/JP2006/325843 patent/WO2007086223A1/ja active Application Filing
- 2006-12-26 EP EP06843227A patent/EP1978011A4/en not_active Withdrawn
-
2007
- 2007-01-03 TW TW096100212A patent/TW200728265A/zh unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH06107581A (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 |
JPH09194414A (ja) * | 1996-01-11 | 1997-07-29 | Mitsubishi Chem Corp | ビスフェノールaの製造方法 |
JP2002534402A (ja) | 1999-01-07 | 2002-10-15 | バイエル アクチェンゲゼルシャフト | ビスフェノールaプリルの製造方法及び製造装置、並びにそれに従って製造されるビスフェノールaプリル |
Non-Patent Citations (2)
Title |
---|
NAKAMURA K.: "Kagaku Kojo ni okeru Sochi. Kiki Toriatsukaiho", vol. 1ST ED., 1973, pages: 86 - 90, XP003017954 * |
See also references of EP1978011A4 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103275335A (zh) * | 2013-05-20 | 2013-09-04 | 安徽理工大学 | 一种聚乙烯蜡微粉的制备方法及喷雾造粒系统 |
Also Published As
Publication number | Publication date |
---|---|
EP1978011A4 (en) | 2010-12-01 |
JP2007197391A (ja) | 2007-08-09 |
EP1978011A1 (en) | 2008-10-08 |
TW200728265A (en) | 2007-08-01 |
CN101336221A (zh) | 2008-12-31 |
RU2008134904A (ru) | 2010-03-10 |
KR20080090455A (ko) | 2008-10-08 |
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