美国专利US20010007014A1 Process and apparatus for producing polycarbonate

专利PDF首页>>美国专利

专利附录

专利说明

权利要求

类似技术

同族专利

引用文献

法律状态

优先权

专利摘要:
A process for producing polycarbonate designed to improve the quality of polycarbonate as a polymerization product polymer and reduce the investment and operating costs is provided. Polycarbonate is produced in two horizontal cylindrical agitation reactors provided with agitation blades successively extended through the vessel and partly with agitation blades having a screw function, as horizontally ganged together in series without any agitator center shaft, where the primary agitation reactor is a uniaxial horizontal agitation reactor with the agitation blades rotating at a low speed ranging from 1 rpm to 10 rpm, while keeping a clearance between the inner wall of the vessel ad the agitation blades in a range of 1 mm to 50 mm, and the secondary agitation reactor is a biaxial horizontal agitation reactor with agitation blades provided horizontally and in parallel, without any rotating center shaft, which conducts treatment by agitation at a low speed ranging from 1 rpm to 15 rpm.
公开号:US20010007014A1
申请号:US09/790,514
申请日:2001-02-23
公开日:2001-07-05
发明作者:Takatoshi Kinoshita；Kazunori Harada；Seiji Motohiro
申请人:Takatoshi Kinoshita；Kazunori Harada；Seiji Motohiro；
IPC主号:B01F7-00583

专利说明:
[0001] This application is a Divisional application of Ser. No. 09/486,913, filed Oct. 12, 2000, which is an application filed under 35 USC 371 of International application No. PCT/JP98/05245, filed Nov. 20, 1998. [0001] TECHNICAL FIELD
[0002] The present invention relates to a process and an apparatus for producing polycarbonate, which is suitable for producing polycarbonate from diphenyl carbonate and an alcohol such as bisphenol A, etc. as raw materials by transesterification upon mixing with a reaction catalyst and additives such as a color adjustment, etc. [0002] BACKGROUND ART
[0003] In a process using vertical agitation reactors as disclosed in “Polycarbonate Resin”, page 66, published by Nikkan Kogyo Shinbun, a larger number of agitation reactors are required for continuous production with increasing scale of the facility, rendering the process uneconomical. [0003]
[0004] From the viewpoint of a model for perfect mixing vessels ganged together in series as an economical apparatus structure, it is effective to use horizontal agitation reactors capable of providing a large number of such perfect mixing vessels. [0004]
[0005] A spectacle rim-formed polymerization apparatus as disclosed in FIG. 2.[0005] 49(b), C1-43, C·Engineering section, of Mechanical Engineering Handbook, is a continuous agitation reactor, which can provide ideal extrusion flow characteristics, that is, a large number of perfect mixing vessels as ganged together in series, but the highly viscous liquid, when treated therein, tends to attach to the surface of the agitator center shaft and reside thereon with increasing liquid viscosity. That is, no sharp residence time distribution function curve can be obtained. Its mode is shown by a delta response curve in FIG. 8, which is based on test data on relations between the number of model vessels for perfect mixing vessels as ganged together in series and the residence time distribution function. In the spectacle rim-formed polymerization apparatus, deviation from the theoretical curve occurs around the point where the dimensionless number of time, t/to, exceeds 1.3. This means that a portion of the liquid resides in the dead zone of agitation, resulting in a problem of polymer quality deterioration. DISCLOSURE OF THE INVENTION
[0006] An object of the present invention is to provide a process and an apparatus for producing polycarbonate, which can improve the quality of polycarbonate as a polymerization product polymer. [0006]
[0007] Another object of the present invention is to provide a process and an apparatus for producing polycarbonate, designed to reduce the investment and operating costs. [0007]
[0008] According to one aspect of the present invention, a process for producing polycarbonate is provided, which comprises subjecting diphenyl polycarbonate and an alcohol such as bisphenol A, etc. as raw materials to polycondensation reaction at elevated temperatures ranging from 200° C. to 300° C. in vacuum less than or equal to the atmospheric pressure in one or more horizontal cylindrical agitation reactors, as ganged together in series, without any agitator center shaft, with increasing liquid viscosity from 1 Pa·s to 5,000 Pa·s, thereby continuously producing polycarbonate. [0008] BRIEF DESCRIPTION OF THE DRAWINGS
[0009] FIG. 1 is a schematic process diagram showing one embodiment of the present process for producing polycarbonate. [0009]
[0010] FIG. 2 is a side view showing one embodiment of the agitation blade structure of a primary agitation reactor. [0010]
[0011] FIGS. [0011] 3 to 7 are front views each showing embodiments of partition plates.
[0012] FIG. 8 is a mixing characteristic diagram showing one example of delta response curve. [0012]
[0013] FIG. 9 is a characteristic diagram showing one example of relations between the viscosity and the number of theoretical plates. [0013]
[0014] FIG. 10 is a characteristic diagram showing one example of relations between the viscosity and the miscibility. [0014] BEST MODE FOR CARRYING OUT THE INVENTION
[0015] Lattice blade polymerization apparatus is an agitation reactor having rectangular frames as ganged together without any agitator center shaft, as disclosed, for example, in JP-B-6-21159, which can show a curve along the theoretical values. [0015]
[0016] For continuous treatment of a highly viscous liquid, it is obvious from said fact that agitation blades without any agitator center shaft have a better-miscibility and can contribute to improvement of product liquid quality. Therefore, for continuous production of polycarbonate from diphenyl carbonate and an alcohol such as bisphenol A, etc. as raw materials with elevated liquid viscosity, it is preferable to conduct polycondensation continuously in one or more horizontal cylindrical agitation reactors, as ganged together in series, without any agitator center shaft, at elevated temperature ranging from 200° C. to 300° C. in vacuum less than or equal to the atmospheric pressure with increasing liquid viscosity from 1 Pa·s to 5,000 Pa·s. [0016]
[0017] FIG. 9 shows test data of miscibilities of various horizontal agitation reactors in comparison. [0017]
[0018] The larger the number of theoretical plates per unit stage, the better the miscibility and the smaller the apparatus size, i.e. the more economical. In FIG. 9, the uniaxial agitation reactor is an agitation reactor without any agitator center shaft, where agitation blades are continuously extended, while keeping the clearance between the blade outer edges and the inner wall of the vessel in a range of 1 mm-50 mm all over the inner surface of the vessel. It is obvious from the result of said data that the uniaxial agitation reactor can involve larger numbers of perfect mixing vessels than that of the spectacle rim-formed polymerization apparatus and thus has a better miscibility. FIG. 10 also shows miscibilities. It is obvious therefrom that at a higher viscosity than 400 Pa·s-600 Pa·s the miscibility of spectacle rim-formed blades becomes poorer than that of lattice blades. That is, it is obvious from the test data of FIGS. 9 and 10 that a horizontal agitation reactor without any agitator center shaft is more effective for treating a highly viscous liquid ranging from 1 Pa·s to 5,000 Pa·s. [0018]
[0019] FIG. 1 shows one embodiment of a process for producing polycarbonate. In a continuous process for producing polycarbonate from diphenyl carbonate and bisphenol A as raw materials by transesterification, the liquid viscosity will increase with the progress of reaction. Prepolymer having a viscosity of 1 Pa·s or higher obtained by the initial polycondensation reaction at the preliminary stage is continuously fed to primary agitation reactor [0019] 1 by pump 6. The agitation reactor for this purpose is a horizontal agitation reactor in an agitation structure without any agitator center shaft, as shown, for example, in FIGS. 2 to 7. Rotating axes 19 at both ends are connected to end plates 22, respectively, and both end plates are secured to each other by a few reinforcing members 24. A plurality of blade partition plates 10 to 13 having different shapes depending on liquid viscosity ranges are provided in the vertical direction to reinforcing member 24 between both end plates 22 to prevent the liquid from short pass in the longitudinal direction and arranged at broader and broader distances in proportion to increasing viscosity ranges. Numeral 12 designates an intermediate plate.
[0020] Agitation blades [0020] 15, 16, 17 and 18 have different blade widths depending upon the liquid viscosity ranges and different numbers of blades provided around the inner wall. Agitation blades are continuously extended and arranged in the longitudinal direction, while keeping small clearances ranging from 1 mm to 50 mm from the inner wall of vessel 50. Rotating axes rotate at a lower speed of 1 rpm-10 rpm in comparison with a speed of 15 rpm-20 rpm as used in the case of the polymerization apparatus with spectacle rim-formed blades. As a result, the agitation power can be reduced to a few tenths. Scraper blades 20 and 21 provided on the outer side of both end plates 22, respectively, have a screw function of pushing the liquid back inwardly, while keeping a small clearance from the inner wall of the vessel proper.
[0021] The liquid having a viscosity of about 1,000 Pa·s discharged from the primary agitation reactor [0021] 1 is fed to secondary agitation reactor 2 by pump 6. The secondary agitation reactor is a biaxial agitation reactor provided with successively linked agitation blades of rectangular frames horizontally and in parallel without any agitator center shaft, as disclosed in JP-B-6-21159. The reaction further proceeds in this reactor, where the liquid viscosity is elevated to about 5,000 Pa·s, continuously producing polymers.
[0022] In both agitation reactors, polycondensation reaction is carried out at elevated temperatures ranging from 200° C. to 350° C. in vacuum ranging from the atmospheric pressure to 0.1 Torr. Phenol as a reaction by product is discharged from the agitation reactors as overhead vapor to the system outside after condensation in condenser [0022] 4.
[0023] According to another embodiment, the same type as that of primary agitation reactor [0023] 1 is used for secondary agitation reactor 2, where blade partition plates having different shapes depending upon the liquid viscosity ranges are arranged at broader and broader distances in proportion thereto. As a result, the agitation power can be further reduced.
[0024] According to the present invention, the product liquid quality can be improved by using a horizontal agitation reactor or reactors with successively linked agitation blades without any rotating center shaft. The present invention can also provide a process for producing polycarbonate, which can reduce the investment and operating costs. [0024]

权利要求:
Claims (4)
[1" id="US-20010007014-A1-CLM-00001] 1. An apparatus for producing polycarbonate, comprising:
a first stage reactor and a second stage reactor, and supply structure for supplying diphenyl carbonate and an alcohol to the first stage reactor and a mixed liquid from the first stage reactor to the second stage reactor,
wherein the first stage reactor is a uniaxial horizontal agitation reactor comprising a horizontal cylindrical vessel and agitation blades annularly distributed and successively arranged through the vessel and secured at positions deviated from a rotating axis toward the inner wall of the vessel without any agitator center shaft,
wherein the second stage reactor is a horizontal biaxial agitation reactor with lattice blades,
wherein each of the first and second stage reactors includes a heater for heating the respective stages to a temperature ranging from 200° C. to 300° C., and
wherein each of the first and second stage reactors includes structure to provide a pressure in the respective reactor equal to or less than atmospheric pressure,
so as to thereby conduct polycondensation reaction of the diphenyl carbonate and the alcohol and continuously produce polycarbonate.
[2" id="US-20010007014-A1-CLM-00002] 2. An apparatus for producing polycarbonates according to
claim 1 , wherein the alcohol is bisphenol A.
[3" id="US-20010007014-A1-CLM-00003] 3. A process for producing polycarbonate, which comprises a first step of subjecting a mixed liquid of diphenyl carbonate and an alcohol to agitating and mixing treatment in a uniaxial horizontal agitation reactor without any agitator center shaft and a second step of subjecting the mixed liquid from the first step to agitation and mixing treatments in a horizontal biaxial agitation reactor with lattice blades, both steps being carried out at elevated temperatures ranging from 200° C. to 300° C. in vacuum less than or equal to the atmospheric pressure with increasing viscosity from 1 Pa·s to 5,000 Pa·s, thereby conducting polycondensation reaction of the mixed liquid and continuously producing polycarbonate.
[4" id="US-20010007014-A1-CLM-00004] 4. The process for producing polycarbonate according to
claim 3 , wherein said alcohol is bisphenol A.

类似技术:

公开号 | 公开日 | 专利标题

US6329495B2|2001-12-11|Process and apparatus for producing polycarbonate

US6846103B2|2005-01-25|Apparatus for continuous stirring and process for continuous polycondensation of polymer resin

JP3847765B2|2006-11-22|Continuous production method of polybutylene terephthalate

US4613664A|1986-09-23|Process for production of polyester

EP1498175A1|2005-01-19|Apparatus and method for discontinuous polycondensation

GB2089361A|1982-06-23|Process and apparatus for the continuous production of polyester

US6350848B1|2002-02-26|Process and apparatus for producing polycarbonate

US4419488A|1983-12-06|Process for continuous production of high impact polystyrene

JP3630109B2|2005-03-16|Method for producing polycarbonate

JP3603822B2|2004-12-22|Method for producing polycarbonate

JP2000344874A|2000-12-12|Method and apparatus for producing polybutylene terephthalate

JP2001031754A|2001-02-06|Manufacture of polycarbonate resin

JP3264258B2|2002-03-11|Method and apparatus for producing polycarbonate

JP2000007772A|2000-01-11|Continuous production apparatus and process for polycondensation polymer

JP3489554B2|2004-01-19|Continuous production equipment for polybutylene terephthalate

JP3216832B2|2001-10-09|Manufacturing method of aromatic polycarbonate

JPH10218998A|1998-08-18|Production of polycondensation polymer

JPH10218985A|1998-08-18|Production of aromatic polycarbonate

EP1369169B1|2006-09-06|Apparatus for continuous stirring and use for continuous polycondensation of polymer resin

JPH11335453A|1999-12-07|Production of poly| and manufacturing equipment

JPH08311207A|1996-11-26|Apparatus and method for continuously producing polycondensation polymer

KR19990065400A|1999-08-05|Polyester final reactor

EP0626411A1|1994-11-30|Method and apparatus for increasing viscosity uniformity in polycarbonate manufacture

JPH093200A|1997-01-07|Apparatus for continuous production of polycondensation polymer and method therefor

JP2001031753A|2001-02-06|Manufacture of polycarbonate resin

同族专利:

公开号 | 公开日

US6265525B1|2001-07-24|

ES2193580T3|2003-11-01|

JPH11158262A|1999-06-15|

EP1002820B1|2003-05-14|

WO1999028370A1|1999-06-10|

EP1002820A4|2000-10-18|

KR100326726B1|2002-03-12|

DE69814643D1|2003-06-18|

DE69814643T2|2004-03-25|

TW495522B|2002-07-21|

KR20010023969A|2001-03-26|

US6329495B2|2001-12-11|

EP1002820A1|2000-05-24|

引用文献:

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

US20050131197A1|2003-12-06|2005-06-16|Uwe Hucks|Transesterification process for the production of polycarbonates having a low content of volatile compounds|

US20120065355A1|2010-09-10|2012-03-15|Mega Data Gmbh|Polymerization of High Viscosity Materials|

US20170030031A1|2015-07-29|2017-02-02|Uniwersytet Wroclawski|Stabilizing composition to stabilize clay land and clay soils, its method of manufacture and stabilization of clay land and clay soils|BE634002A|1962-07-30||||

NL7103449A|1971-03-15|1972-09-19|||

FR2130950A5|1971-03-26|1972-11-10|Creusot Loire||

US3776473A|1972-03-27|1973-12-04|Int Nickel Co|Highly reflective aluminum flake|

JPS5730531B2|1974-06-10|1982-06-29|||

JPH0311299B2|1985-11-11|1991-02-15|Hitachi Ltd||

LU86396A1|1986-04-18|1986-09-02|Pharma Roche Posay Lab|COMPOSITIONS FOR THE TREATMENT OF Baldness and Alopecia|

JP2628905B2|1988-12-06|1997-07-09|日本ジーイープラスチックス株式会社|Method for producing polycarbonate|

JP3401732B2|1994-03-07|2003-04-28|出光石油化学株式会社|Method for producing polycarbonate|

JP3193266B2|1995-06-13|2001-07-30|帝人株式会社|Method for producing aromatic polycarbonate|

JP3628110B2|1996-06-18|2005-03-09|株式会社神戸製鋼所|Horizontal reactor for stirring high viscosity substances|US6197436B1|1997-10-23|2001-03-06|Jamar Venture Corporation|Method and composition for diffusion alloying of ferrous materials|

US7163334B2|2000-03-13|2007-01-16|The University Of Akron|Method and apparatus for mixing fibers|

DE10119851A1|2001-04-24|2002-10-31|Bayer Ag|Process for the continuous production of polycarbonates by the melt transesterification process|

EP1369169B1|2002-06-07|2006-09-06|Hitachi Ltd.|Apparatus for continuous stirring and use for continuous polycondensation of polymer resin|

JP4112908B2|2002-06-07|2008-07-02|株式会社日立プラントテクノロジー|Continuous stirring device and continuous polycondensation method of polycondensation resin|

US6974260B2|2003-07-30|2005-12-13|Emcore Corporation|Flexible substrate for routing fibers in an optical transceiver|

JP2005314503A|2004-04-28|2005-11-10|Hitachi Ltd|Method and apparatus for continuously concentrating/condensing hydroxycarboxylic acid|

DE102007022130B4|2007-05-11|2015-02-19|Bayer Intellectual Property Gmbh|Process for the preparation of polycarbonate after the melt transesterification process|

DE102007052968A1|2007-11-07|2009-05-14|Bayer Materialscience Ag|Process for the preparation of polycarbonate after the melt transesterification process|

DE102008011903A1|2008-02-29|2009-09-03|Bayer Materialscience Ag|Polycarbonates with cyclic oligomers and improved flow behavior|

DE102008019503A1|2008-04-18|2009-10-22|Bayer Materialscience Ag|Polycarbonates with rearrangement structures, cyclic and linear oligomers and improved flow behavior|

WO2011120198A1|2010-04-01|2011-10-06|Bayer Materialscience Ag|Melt polycarbonate having improved heat ageing resistance and manufacturing method thereof|

KR101612159B1|2013-06-21|2016-04-12|제일모직주식회사|Apparatus and method for continuous solid state polymerization|

KR101657271B1|2013-07-10|2016-09-13|롯데첨단소재|Apparatus and method for continuous solid state polymerization|

CN107207842B|2014-12-04|2019-11-05|科思创德国股份有限公司|Polycarbonate compositions containing polyethylene wax|

US20190143582A1|2016-05-04|2019-05-16|Covestro Deutschland Ag|Copolycarbonate as a supporting material in 3-d printing|

CN108948340B|2018-06-05|2021-03-09|金聚合科技有限公司|Device and method for preparing aromatic polycarbonate|

EP3581605A1|2018-06-14|2019-12-18|Covestro Deutschland AG|Melting ester interchange method for simultaneously producing at least two different polycarbonates in a production plant|

WO2021023690A1|2019-08-08|2021-02-11|Covestro Intellectual Property Gmbh & Co. Kg|Process for the preparation of a polycarbonate|

EP3838979A1|2019-12-17|2021-06-23|Covestro Deutschland AG|Melt polycarbonate with improved optical properties|

法律状态:
2001-11-21| STCF| Information on status: patent grant|Free format text: PATENTED CASE |

2003-07-22| CC| Certificate of correction|

2005-05-28| FPAY| Fee payment|Year of fee payment: 4 |

2007-03-05| AS| Assignment|Owner name: HITACHI PLANT TECHNOLOGIES, LTD., JAPAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:HITACHI, LTD.;REEL/FRAME:019000/0373 Effective date: 20061030 |

2009-05-22| FPAY| Fee payment|Year of fee payment: 8 |

2013-03-08| FPAY| Fee payment|Year of fee payment: 12 |

优先权:

申请号 | 申请日 | 专利标题

JP09-327582||1997-11-28||

JP9327582A|JPH11158262A|1997-11-28|1997-11-28|Production of polycarbonate|

US09/486,913|US6265525B1|1997-11-28|1998-11-20|Method and device for manufacturing polycarbonate|

US09/790,514|US6329495B2|1997-11-28|2001-02-23|Process and apparatus for producing polycarbonate|US09/790,514| US6329495B2|1997-11-28|2001-02-23|Process and apparatus for producing polycarbonate|

US09/940,884| US6350848B1|1997-11-28|2001-08-29|Process and apparatus for producing polycarbonate|

US10/082,239| US6753403B2|1997-11-28|2002-02-26|Process and apparatus for producing polycarbonate|

[返回顶部]