CN1119226C - 塑料特别是高分子聚碳酸酯溶液的脱气装置和方法 - Google Patents
塑料特别是高分子聚碳酸酯溶液的脱气装置和方法 Download PDFInfo
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- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
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Abstract
本发明涉及了用双轴挤压机对塑料特别是高分子聚碳酸酯溶液脱气的装置,双轴挤压机有同向转动的互相啮合的轴。该装置的特征在于,挤压机的长度/直径比小于/等于40,在挤压机的排气区轴设计成二行程,而在压力形成区轴设计成三行程。该装置能经济地制备具有特别高的光透射率的聚碳酸酯。此外还涉及相应的方法。
Description
本发明涉及利用双轴挤压机对塑料特别是高分子聚碳酸酯的脱气的装置和方法,该双轴挤压机有同向转动的互相啮合轴。
随着环保意识的提高,在塑料加工中对除去合成材料中的挥发性成分的要求也日益提高。特别是在食品领域中的塑料应用。在挤压的塑料中挥发性成分不允许超过0.2重量%,为了改善产品质量,特别是光学性能,还必须全部除去挥发性成分。这对具有氯苯和二氯甲烷作为挥发成分的高分子聚碳酸酯溶液的产品是特别重要的。从聚合物中除去挥发性成分在塑料工业中称为脱气。为了脱气可应用各种装置,特别是单螺杆或双螺杆挤压机。
在用单螺杆或双螺杆挤压机的脱气过程中,可分为向前或向后脱气过程或一次或多次脱气过程。对于向前脱气过程,挤压机的排气口安装在挤压机螺杆推进方向的进料口下游,而在向后排气过程中,排气口安装在螺杆推进方向的进料口上游。也可用脱气挤压机,这时不仅达到向前脱气而且也进行向后脱气。根据所除去的挥发性成分的剩余含量可进行一级或多级脱气过程。然而脱气过程的级数不能随意增加,因为这要提高产品制备成本而且常常降低产品质量。产品质量特别取决于过程温度或温度的提高以及要脱气的塑料在挤压机中的停留时间。
本发明的目的是提供上述类型的设备和方法,该设备和方法能导致产品质量的改善且成本也适宜,并且使得具有特别高的光透射性的聚碳酸酯的制备成为可能。
这个目的根据发明按如下达到,挤压机的轴在脱气区域是双进程的,而在压力形成区域是三行程的,挤压机的L/D-比小于/等于40,在此L代表螺杆长度,D代表螺杆直径。
通常的脱气挤压机例如可使得高分子聚碳酸酯的光的透射率为87-88。而按照本发明的装置或者相应的方法可使得这些高分子聚碳酸酯类的光的透射率达到令人意外的88.5-89.5。
此外能够降低产品制备成本,因为按照本发明的装置的挤压机是较短的,结果就相应地减少了占地面积和设备的成本。
用L/D-比为35-40的双螺杆挤压机可获得特别高的光透射率值。
为避免温度相关的对质量损害,如果挤压机具有界定冷却区的冷却设备是有益的。以这种方式对产品质量有正面的影响。在冷却区挤压机的轴最好设计三行程的。
另一个优选的方式是直接在挤压机的进料口下游的轴的推进部件之间安装捏和部件。该捏和部件用作为引入能量,特别是用来扩大脱气表面。
如果按照另一种方式,挤压机在推进方向有多个脱气区域,在每个区域都连接有抽气设备,那么就可获得特别高的脱气率。在挤压机的推进方向有三个脱气区域的挤压机能获得非常好的结果,在此,为第一个脱气区域安装的排气口处产生的绝对压力为0.5-1.5bar,在第二个脱气区域安装的排气口处产生的绝对压力为0.03-1.9bar,在第三个脱气区域安装的排气口处产生的绝对压力为0.001-0.03bar。
此外采用扩大脱气表面的夹带剂可对脱气产生正面的影响。根据本发明的方法,夹带剂优选在推进方向的第二和第三脱气区域之间被加入。氮气优选用作为夹带剂。在轴转数小于/等于390U/min时,所加入氮气体积流量应优选为2-10Nm3/h。
本发明的其他的优越方式在从属权利要求中给出。
下面用说明实施例的附图来更详细地解释本发明。该图图示按照本发明装置的双轴挤压机的纵向剖面图。
双轴挤压机有由总共八个部件组成的外壳,在这个外壳里面安装有同向转动的、互相啮合的轴(未示出)。要脱气的塑料通过在第一个外壳部件1中形成的进料口2而被输送入挤压机中。按推进方向,在进料口2的上游安装有排气口3(向后排气)。轴的驱动端是通过在图中第一个外壳部件2的左侧的转动环密封(未示出)而向外引导的。
在推进方向与第一个外壳部件1连接着长度大约相同的第二个外壳部件4,在此有另一个排气口5。接着是第三个较长的外壳部件6,其通过第四个较短的外壳部件7连接到第五个外壳部件8,这第五个外壳的长度与第三个外壳部件6相当。第三第五外壳部件每个都有相同大小的排气口9、10,这二个排气口的长度是第二个外壳部件4的排气口5的二倍多。排气口5、9、10与抽气装置(未示出)相连接。
第四个外壳部件7有接口11,通过该接口夹带剂优选为氮气被混入。
在第五个外壳部件8下游是三个基本同样大小的外壳部件12、13、14,这里形成压力形成区域,在其末端被脱气的产品从挤压机排出。从图中可以看到,在第六个外壳部件12有一个接口15,该接口可连接侧挤压机,通过它可对脱气产品加入添加物。
在压力形成区域,该轴是三行程形式。
直接在进料口2下游,轴的推进部件之间安装有捏和部件。在外壳部件1、4、6、7和8的区域内,轴呈二行程。二行程和三行程的轴优选具有不同的倾斜角或倾斜方向。
按照本发明的装置,其运行状况如下,在第一个排气口3的绝对压力为1-2bar,在第二个排气口5的绝对压力为2.5-1.5bar,在第三个排气口9的绝对压力为0.03-0.9bar,而在第四个排气口10的绝对压力为0.00-0.03bar。
双轴挤压机优选的转数为小于/等于390U/min。所加入的氮体积流量优选为2-10Nm2/h。
为了防止温度相关的质量损害,挤压机安置有冷却设备(未示出)。该冷却设备优选地安置于外壳部件12、13、14区域中。
已经表明,采用这类结构装置可生产有特别高光透射率的聚碳酸酯,即对于高分子聚碳酸酯(V-数为1.33),其光的透射率为88.5-89.5。
Claims (22)
1.一种用双轴挤压机对塑料脱气的装置,该双轴挤压机具有同向转动的互相啮合的轴,其特征在于,挤压机的长度/直径比为小于/等于40,轴在挤压机排气区设计成二行程,而在压力形成区设计成三行程。
2.根据权利要求1的装置,其特征在于,其长度/直径比为35-40。
3.根据权利要求1或2的装置,其特征在于,挤压机还有界定的冷却区的冷却设备。
4.根据权利要求3的装置,其特征在于,在冷却区内轴设计成三行程。
5.根据上述权利要求之一的装置,其特征在于,直接在挤压机的进料口(2)的下游的轴推进部件之间安装有捏和部件。
6.根据上述权利要求之一的装置,其特征在于,挤压机在推进方向有多个排气区,在每个排气区与抽气装置连接。
7.根据上述权利要求之一的装置,其特征在于,在二个排气区之间的区域,轴呈三行程。
8.根据上述权利要求之一的装置,其特征在于,在二个排气区之间挤压机安装有夹带剂进入口(11)。
9.根据权利要求8的装置,其特征在于,挤压机在推进方向有三个排气区,夹带剂入口安置在第二和第三排气区之间。
10.根据上述权利要求之一的装置,其特征在于,在挤压机的进料口(2)之前安装有用于向后脱气的排气口(3)。
11.根据上述权利要求之一的装置,其特征在于,在推进方向的最后的排气区下游安装有加入添加物的加料设备(15)。
12.一种用双轴挤压机对塑料脱气的方法,该挤压机具有同向转动的互相啮合的轴,其特征在于,在挤压机的排气区内轴设计成二行程,而在压力形成区内轴设计成三行程,并且挤压机的长度/直径比为小于/等于40。
13.根据权利要求12的方法,其特征在于,长度/直径比为35-40。
14.根据权利要求12或13的方法,其特征在于,塑料经冷却。
15.根据权利要求14的方法,其特征在于,在冷却区内轴设计成三行程。
16.根据权利要求12-15之一的方法,其特征在于,塑料的脱气是以向前脱气或向前脱气和向后脱气的组合方式进行,向前脱气过程以多级进行,在每一脱气级中,采用抽气装置排除塑料的挥发成分。
17.根据权利要求12-16之一的方法,其特征在于,挤压机在推进方向有三个排气区,在第一个排气区安装的排气口(5)的绝对压力为0.5-1.5bar,在第二个排气区安装的排气口(9)的绝对压力为0.03-1.9bar,在第三个排气区安装的排气口(10)的绝对压力为0.001-0.03bar。
18.根据权利要求12-17之一的方法,其特征在于,在塑料中混入夹带剂。
19.根据权利要求18的方法,其特征在于,在推进方向的第二和第三排气区之间混入夹带剂。
20.根据权利要求18或19的方法,其特征在于,采用氮气作为夹带剂。
21.根据权利要求20的方法,其特征在于,挤压机的转数为小于/等于390U/min,所混入的氮气体积流量为2-10Nm3/h。
22.根据权利要求12-21之一的方法,其特征在于,在推进方向的最后排气区连接有压力形成区。
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DE102004041689B4 (de) * | 2004-08-27 | 2010-02-11 | Kraussmaffei Berstorff Gmbh | Vorrichtung zur Herstellung von Spritzgussteilen |
DE102007029010A1 (de) * | 2006-08-26 | 2008-02-28 | Bayer Materialscience Ag | Verfahren zum Compoundieren von Polymeren |
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EP2255947A1 (de) | 2009-05-30 | 2010-12-01 | Bayer MaterialScience AG | Vorrichtung und Verfahren zum Mischen von Polymerschmelzen mit Additiven |
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-
1999
- 1999-03-27 DE DE19914143A patent/DE19914143A1/de not_active Ceased
-
2000
- 2000-03-13 TW TW089104458A patent/TW548174B/zh not_active IP Right Cessation
- 2000-03-14 WO PCT/EP2000/002240 patent/WO2000058072A1/de not_active Application Discontinuation
- 2000-03-14 EP EP00914132A patent/EP1165302B1/de not_active Expired - Lifetime
- 2000-03-14 JP JP2000607807A patent/JP4434497B2/ja not_active Expired - Lifetime
- 2000-03-14 BR BR0009367-0A patent/BR0009367A/pt not_active IP Right Cessation
- 2000-03-14 ID IDW00200102307A patent/ID30399A/id unknown
- 2000-03-14 AU AU35557/00A patent/AU3555700A/en not_active Abandoned
- 2000-03-14 CN CN00805518A patent/CN1119226C/zh not_active Expired - Lifetime
- 2000-03-14 ES ES00914132T patent/ES2192521T3/es not_active Expired - Lifetime
- 2000-03-14 US US09/937,467 patent/US6811294B1/en not_active Expired - Lifetime
- 2000-03-14 DE DE50001239T patent/DE50001239D1/de not_active Expired - Lifetime
- 2000-03-14 KR KR1020017012257A patent/KR20010108409A/ko not_active Application Discontinuation
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2002
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Also Published As
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JP4434497B2 (ja) | 2010-03-17 |
DE19914143A1 (de) | 2000-09-28 |
HK1045665B (zh) | 2004-05-14 |
CN1345265A (zh) | 2002-04-17 |
EP1165302B1 (de) | 2003-02-12 |
DE50001239D1 (de) | 2003-03-20 |
US6811294B1 (en) | 2004-11-02 |
ES2192521T3 (es) | 2003-10-16 |
KR20010108409A (ko) | 2001-12-07 |
BR0009367A (pt) | 2001-12-26 |
HK1045665A1 (en) | 2002-12-06 |
ID30399A (id) | 2001-11-29 |
WO2000058072A1 (de) | 2000-10-05 |
EP1165302A1 (de) | 2002-01-02 |
JP2002539987A (ja) | 2002-11-26 |
AU3555700A (en) | 2000-10-16 |
TW548174B (en) | 2003-08-21 |
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