CN1190356A - 用于传质塔中的具有低压降和有序结构的织物填料或织物状填料以及使用这些填料的精馏方法 - Google Patents
用于传质塔中的具有低压降和有序结构的织物填料或织物状填料以及使用这些填料的精馏方法 Download PDFInfo
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- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
本发明涉及用于物质交换塔装置中的填料元件,该填料元件具有低的压力损失,其直径为该塔的内径和高度在40—300毫米之间。这些填料元件由具有有序结构的、相互接触的和尺寸稳定的层(2,3)构成,该填料元件由织物或织物状材料制成。填料元件的特征在于:a)织物或织物状材料、优选金属材料的相互接触的成型了的层是这样安装的,以致它们形成许多窄的流动通道,优选几乎是三角形、长方形、方形或等边六角形通道,填料的各个织物层(2,3)的齿面与塔轴倾斜角(1)仅为0—25°,优选3—14°;和b)为了确保填料元件的机械稳定性,在织物层(2,3)之间适当排列安装金属线或细的连杆(4),或者在一些接触点固定连接织物层。本发明还涉及通过使用新的填料元件的精馏从混合物中得到纯物质的方法。
Description
本发明涉及用于传质塔的填料元件和由这些填料形成的塔内构件,这些填料由织物材料或织物状材料、优选金属织物制成,并且具有有序结构和新的几何结构,这些填料用于传质塔中,具有特别低的单位压降,本发明还涉及这些填料在混合物精馏方法中的应用。
在逆流蒸馏的情况下,通过蒸馏处理产物混合物,通常可得到好的结果,逆流蒸馏也称作精馏,即这样一种蒸馏方法,其中液体在塔中作为回流从上向下流动,而蒸气由下向上流动,这样就使得蒸气中富含易挥发组分,而液体中富含不易挥发的组分。
这种传质和传热是通过安装在塔内的元件,如塔板或填料来强化的,这些塔内单元确保了各相之间有足够的接触时间,并且足够增大了相的界面积。然而,这些塔内部构件和向下流动的回流一起对在塔中的蒸气的流动产生了阻力,该阻力叫做压降。对于给定的塔几何结构,即塔内径和塔高,塔内的压降不仅取决于要精馏的化合物的性质和量,而且还极大地取决于塔内构件的特征。
通常,对要求具有高的分离效果的混合物,所用的分馏装置是具有内部构件的精馏塔,其内部构件由具有有序结构的金属织物制成。这种填料以有次序的、有规律的几何结构构成,并对通过的逆流相具有确定的面积,这些填料不同于所有其它的内部构件,因为它们能够具有更高的流速、更好的分离效果和更低的单位压降。因此,它们可用于所有的减压精馏中,其中,因为待分离的混合物的温度敏感性,所以限制塔中的压降是特别重要的。特别适合的塔填料是如下的填料:Sulzer(参看Sulzer公司出版物“用于蒸馏和吸收的分离塔”)提供的BX和CY型金属织物填料,和由其他公司提供的具有相似效果的金属织物填料,例如Montz GmbH的Montz-Pak型A3和织物状填料,例如Montz GmbH的BSH型填料。
这种塔的图示可在下面教课书中找到,例如教课书“热分离方法”Klaus Sattler,VCH出版公司,Weinheim(FRG),1988)的103页。关于混合物精馏的更详细的情况可参看Klaus Sattler的这本教课书的101-225页,特别是120-160和199-214页。
许多高沸点混合物的热承受能力如此低,以致,尽管使用具有有序结构的所述金属织物填料或织物状填料和塔中的塔顶压力仅为0.5-1毫巴,要求具有必要的分离效率的织物填料的压降将使得塔底温度高于待分离的化合物的分解温度。
本发明的目的是,开发具有有序结构的新的织物填料或织物状填料,该填料在具有相同的分离效率的情况下,与现有的各种塔内构件相比,显示出更低的压降,即提供这样的织物填料,它使得要求高分离效率的高沸点、对空气敏感和/或温度敏感的混合物以好的收率通过蒸馏得到分离,但不必使用费用比较高的蒸馏方法例如高真空蒸馏或短程蒸馏;以及开发新的织物填料,由于它具有低的压降,所以通常允许低的塔底温度和在较温和条件下进行蒸馏,或者能增加塔的容量。
本发明涉及具有低压降、用于传质塔内部构件的填料元件,它的直径为塔内径和高为40-300毫米,该填料元件由比表面积为1002000m2/m3、具有新的几何结构的织物材料或织物状材料的尺寸稳定的层构成,该层具有有序结构并相互接触,其特征在于a)相互接触的织物材料或织物状材料的成形层是这样排列的,以致它们形成了许多窄的流动通道,优选实质上是三角形、长方形或者是等边六角形流动通道,其中各个填料织物层的齿面与塔轴的倾斜角仅为0-25°,优选3-14°,特别是4-6°,和b)为了保证填料元件的机械稳定性,如果需要的话,适当地安装金属线或细的连杆,优选在织物层之间水平安装,或者在多个接触点固定连接织物层。
因此,尽管常规织物填料的齿面的倾斜角通常为至少30°,但由填料元件或盘形塔内构件形成的本发明织物填料显示的织物层的齿面与塔轴的倾斜角仅为0-25°,优选3-14°,特别是4-6°。织物层的齿面与塔轴的倾斜角示于图1中,在图1中,1代表织物层的齿面与塔轴的倾斜角,2代表织物层。
正如已知的织物填料那样,相互接触的织物材料或织物状材料的各个成形层是这样排列的,以致当本发明的填料元件的各个织物层或在由其形成的盘形传质塔内构件的各个织物层的齿面与塔轴的倾斜角大于0时,形成的流动通道交替地反向延伸。
本发明还涉及其直径为塔内径和高为40-300毫米的盘形传质塔内构件,该塔内构件由一种或多种由织物材料或织物状材料制成的本发明填料元件构成,还涉及由许多本发明的盘形传质塔内构件相叠构成的塔内构件,各盘形塔内构件以相互约90°角扭转叠放。
与至今已知的或在文献中介绍的所有填料相比,由本发明新的填料元件的填料或盘形塔内部构件形成的填料具有最低的单位压降。单位压降是当蒸气流过一个其高度准确地相当于一个理论塔板的织物填料时的蒸气流动的压降。据制造者声称,目前销售的比表面积为500m2/m3的填料的单位压降,以1Pa的F系数表示时,为0.09-0.11毫巴/nth。这些填料的分离效率为每米填料约5-7块塔板。使用具有与塔轴垂直或仅稍倾斜于塔轴的流动通道的本发明织物填料能降低单位压降约50%,但具有可比的分离效率。
这样使得传质塔的应用范围增大,还使得该传质塔能够对要求高分离效率、高沸点、对空气敏感和/或温度敏感的物质进行精馏,这是因为由于压降的降低,塔底温度可显著降低。
极其令人意外的是,与已知的织物填料相比,本发明的具有与塔轴垂直或仅稍倾斜于塔轴的流动通道的织物填料或织物状填料在具有明显更低的压降的情况下,还显示出相同的分离效率,在该已知的织物填料中,各个织物层齿面的倾斜角为至少30°(参看Sulzer Chemtech提供的织物填料BX,CY,DX和EX),Montz提供的A3型金属织物填料中的波浪形通道的倾斜角被标准化为30-45°,因为已预先假设了,为了达到最佳传质并获得最佳分离效果,除了液相要有较好的分配外,还有必要使气相的横向混合最佳化。
至今已知的唯一的、由具有垂直流动通道的金属织物填料构成的填料体系是Montz GmbH提供的Kloss和Neo-Kloss填料,这些填料由开槽的或波形化的金属织物层状长条构成,这些长条有间隔地螺旋缠绕而形成缠绕的元件。这些长条相应地含有长的垂直环形流动槽,在槽中各个织物层状长条不直接相互接触。虽然这些填料体系比销售的织物填料具有更低的压降,但它们也具有更低的分离效率,因此其每块塔板压降并不低,即单位压降不低。
可用所有适合于制造织物的材料和用于制造织物的常用材料制造本发明具有新的几何结构的填料元件和塔内构件。可以提及的最重要的是由不锈钢(例如DIN1.0330;1.4000;1.4301;1.4401;1.4404;1.4435;1.4439;1.4571等)、Hasteloy C4、铝(例如DIN3.0255)、铜、钛(例如DIN3.7025)、蒙乃尔合金、合成材料如聚丙烯/聚丙烯腈混合织物制得的织物/金属织物,或由玻璃纤维或碳纤维制得的织物。具有比表面积为约100-2000m2/m3,优选为250-1000m2/m3的织物填料有利于使用。优选由相互接触的成形金属织物层形成的织物填料。
织物可用常规方法加工成形。例如形成图2中的A),B)和C)所描绘的形状,其中实线表示各个织物层的上视图,虚线表示确保稳定性的金属线或连杆的上视图。在图2A,2B和2C中,3表示织物层,4表示金属线或连杆。特别好的填料是其中开槽织物层(如图2A所示)形成流动通道的那些填料。
为了确保填料元件的机械稳定性,用直径优选为约1毫米的线或细的连杆、优选金属线或细的金属连杆适当地固定,优选水平地安装在各个织物层之间,为的是防止织物层滑入另一个织物层中。然而,也可通过在几个接触点牢固地连接各个织物层,如通过软焊、焊接或压焊来确保填料元件的机械稳定性。
与所有的填料一样,本发明填料具有好的分离效率的前提是,在进料口的下方或出料口有好的液体分配。在市场上可得到为此用途的非常好的液体分配器,该分配器在每个塔的截面上具有大量的滴液点。为了得到好的液体分配、尤其是对工业规模的塔的液体分配而言,以下作法是有利的,将一个或多个、优选2或3个具有大的织物层齿面的倾斜角的常规盘形内部构件直接安装在液体分配器的下面,然后将由本发明的填料元件形成的塔内构件紧接着安置在其下面。
通常用于精馏的具有有序结构的织物填料是将与所要求的分离效率相应的多个盘形塔内构件(填料层)组合形成的,该内部构件的高度为约15-25厘米。一个填料层通常由许多适当高度的单个成形织物层构成。当其安置在塔中时,为了确保质量分配尽可能地好,在每种情况下,每个填料层以相对于前面的一个填料层互成90°的角度安装。
本发明的填料元件也是或也成形成为盘形传质塔内构件(填料层),当在塔中安装时,在每种情况下,各填料层相对于前面的填料层扭转约90°。填料的高度可以是4-30、优选16-20、特别是16-17厘米。
据生产者声称,目前市场销售的比表面积为500m2/m3的填料的压降用约1Pa的F系数表示时,为每个理论塔板(nth)0.09-0.11毫巴。这些填料的分离系数为每米填料约5-7块塔板。使用具有与塔轴垂直或仅稍倾斜于塔轴的流动通道的本发明织物填料能降低单位压降约50%,但具有相似的分离效率,并使得塔的容量显著增加,或者能够使用较小直径的塔。
因此,本发明还涉及通过精馏混合物、从这些混合物中得到纯物质的方法,该方法的特征在于,使用这样的精馏塔,其中所有的或至少部分盘形塔内构件是由本发明的填料元件形成的,或者,对于具有小的直径和/或从上面可容易地加入织物填料的塔,也使用这种类型的盘形填料元件。
新填料的低单位压降能使传质塔的应用范围得到扩大,还使其能够对在中等减压即在约0.1-2.5毫巴的压力下要求高分离效率的、高沸点、对空气和/或温度敏感物质的混合物进行精馏,这是因为由于压降的降低,塔底温度能够显著降低。
因此,本发明还涉及在中等减压下、在装有具有有序结构的金属织物填料的塔中、通过精馏从要求高分离效率的、高沸点、对空气和/或温度敏感物质的混合物中得到纯物质的方法,其中精馏是在一个塔中进行,a)其中用具有500个/m2或更多个滴液点的通道式分配器进行液体分配,b)其中液体分配器的通道与直接位于这些分配器下部的盘形塔内部构件的织物层成90°角地安装,c)其中两个或多个盘形塔内部构件安装在液体分配器的下面,该内部构件的高度为20-100毫米,其中的织物层各相互呈90°扭转,d)其中所有其余的或其余的盘形塔内部构件的一部分由本发明的填料元件构成,e)其中塔是这样设计的,以致在精馏期间通过塔壁不发生热交换,和f)对于空气敏感物质,塔是这样设计的,以致其实际上可在隔绝空气的情况下操作。
可以提及的、作为要求高分离效率的、高沸点和高空气和/或温度敏感物质混合物的一个例子是合成的维生素E乙酸酯(VEA),在工业上,是通过三甲基氢醌与植醇或异植醇反应,然后用乙酐酯化来制备维生素E乙酸酯,但制备的维生素E乙酸酯中仍含有少量的着色的低沸点和高沸点杂质。因为VEA在人类营养品和保健品中的应用日益增加,所以对该产品纯度的要求变得越来越高。通常,在工业规模中用精馏来纯化产物是非常有利的,但由于VEA的高沸点和在升高温度下的不稳定性,所以对其精馏是非常困难的。这也是为了能够蒸馏VEA而要在尽可能低的温度下进行高真空蒸馏或甚至分子蒸馏的方法基本上过时的原因。
然而,因为在高真空下蒸馏特别是分子蒸馏得到高的纯度不但会具有低蒸馏收率的缺点,而且还极其复杂,因此在投资成本和操作费用两方面都是非常昂贵的,对于VEA的最终纯化来说,即在精馏作为高沸点、对空气和/或温度敏感物质的混合物并含有着色的低沸点和高沸点物质杂质的VEA的情况下,使用新的填料元件和塔内部构件是特别重要的。
涉及这方面的权利要求的特征a)要求保护具有500个或更多滴液点的通道式分配器的液体分配。类似的分配器也被称作毛细管分配器,但该分配器是园的,这些分配器是由Sulzer和Montz销售的和在例如EP512277中所描述的。已知的通道式分配器通常仅具有50-60个滴液点/米2。
使用根据本发明的通道式分配器以两个不同的方式降低了压降,一方面,该分配器产生了迅速的和极其细的分散,因此可更好地利用填料来分布要分离的混合物,另一方面,产生了非常低的滴液密度。
然而,为了达到最佳分离效率,不但要有大量的滴液点,而且相对于填料元件的位置来恰当安装分配器,这是重要的。
一个织物填料层通常由许多其高度为170毫米的织物层逐成构成。在安装时,每个填料层以相对于前面一个填料层互成90°角安装。同样,根据特征b),分配器以相对于直接位于分配器下面的填料元件或相对于位于那里的填料层扭转90°角安装。
然后,液体以一个特定的角度喷洒在这些织物层中的一个层上。流过取决于喷洒角度和两个滴液点之间的间距的一段流程后,在一个织物层上形成了均匀的膜。
当填料在这个点扭转90°角时,可最佳地利用填料,即液体可能最快地分布到所有织物层上。
根据特征c),在液体分配器下面放置2个或多个高度仅为20-100毫米、优选25-50毫米,特别是35-45毫米的填料元件,各填料元件的织物层相互扭转90°。将填料分成具有更低高度的元件,可以达到可能最快的分配,由此可最佳地使用填料于分离。
根据特征f),如果必要的话,精馏实际上在隔离空气下进行。这对空气敏感的混合物是特别重要的,例如在精馏粗维生素E乙酸酯的情况下。因此,绝对有必要使用新研制的特别有效的密封材料,例如Cefilac提供的Helicoflex来密封加工控制设备的法兰和/或开口。使用例如在德国专利DE2710859,DE3912478或DD4407728中所述的卷边焊接密封来密封法兰是特别有利的。
在中等真空蒸馏塔中,仅有少量的物料在循环,因此,热量的任何损失都会立即引起塔壁上不可控制的冷凝,这样就降低了塔的分离效率。根据特征e),可将塔的绝热和保温结合起来,以最好地防止通过塔壁的热交换。这种保温方法的工业实施可以以下列方式有利地实现:将一层金属板夹套附着在塔壳体的第一绝热层上,使该金属板夹套再绝热。然后,将另一个金属板夹套和加热器附着在该绝热层上,最后与外界绝热。然后,通过使塔壳体与第一金属板夹套之间的温差为零来控制加热量。
当使用已知的织物填料时,由于VEA的热不稳定性,可在最大高度为5米的填料塔中精馏VEA。
当使用本发明的塔内部构件时,由于降低了压降,所以对于通过蒸馏来最终纯化VEA来说,也可使用高度高于5米的填料塔。
具有对比例的下列实施例是为了显示本发明具有新几何结构的填料的优点。
将本发明的金属织物填料与已知的、具有相同比表面积的金属织物填料的单位压降Δp/nth进行对比。
在直径为45毫米和长度为1.8米的实验塔中,进行了以下实验:1)用市售的金属织物填料进行比较,该填料是比表面积为500m2/m3的Montz型A3-500填料,其波浪形通道与塔轴的倾斜角为30°,和2)用本发明的金属织物填料,该填料的比表面积为500m2/m3,填料的各个织物层的齿面与塔轴的倾斜角为5°。
在这两种情况下,用一个滴液点进行液体分配,塔顶压力为50毫巴。使用氯代苯/乙基苯混合物作为实验物料。测定具有F系数为0.5-2的单位压降(Δp/nth),结果已作图于图3。
在图3中,曲线1代表Montz型A3织物填料(对比)的压降,曲线2代表本发明的金属织物填料的压降。
曲线表明,本发明的填料显示出明显低的压降,在F=0.5-2 Pa范围内,单位压降仅为具有相同分离效果的Montz型A3-500织物填料的压降的一半。
Claims (10)
1.具有低压降、用于传质塔内部构件的填料元件,其直径为塔的内径和高为40-300毫米,由比表面积为100-2000m2/m3的织物材料或织物状材料的、尺寸稳定的层构成,该层具有有序结构并相互接触,其特征在于
a)相互接触的织物材料或织物状材料的成形层是这样排列的,以致它们形成了许多窄的流动通道,其中各个填料织物层的齿面与塔轴的倾斜角为0-25°,和
b)为了保证填料元件的机械稳定性,如果需要的话,在织物层之间适当地排列安装金属线或细的连杆,或者在多个接触点固定连接织物层。
2.根据权利要求1的用于传质塔内部构件的填料元件,其特征在于,填料元件的各个填料织物层的齿面与塔轴的倾斜角为3-14°。
3.根据权利要求1的用于传质塔内部构件的填料元件,其特征在于,相互接触的结构层是由金属织物或金属的织物状材料形成的。
4.根据权利要求1的用于传质塔内部构件的填料元件,其特征在于,为了保证填料元件的机械稳定性,在各个织物层之间水平排列安装有金属线或细的连杆。
5.根据权利要求1的用于传质塔内部构件的填料元件,其特征在于,相互接触的织物材料或织物状材料的成形了的层是这样排列的,以致它们形成了实质上是三角形、长方形或者是等边六角形流动通道。
6.根据权利要求1的用于传质塔内部构件的填料元件,其特征在于,相互接触的织物材料或织物状材料的成形了的层是这样排列的,以致当的各个织物层的齿面与塔轴的倾斜角大于0时,形成的流动通道交替地反向延伸。
7.用于直径为塔内径和高度为40-300毫米的、用于塔中的盘形传质塔内部构件,该内部构件由一个或许多填料元件构成,该填料元件由如权利要求1所述的、具有有序结构和相互接触的织物材料或织物状材料的、尺寸稳定的层构成。
8.由权利要求7所述的、由多个相互重叠的盘形传质塔内部构件构成的塔内部构件,其中各个盘形塔内部构件相互扭转约90°。
9.一种通过精馏混合物从这些混合物中得到纯物质的方法,其特征在于,使用为此用途的精馏塔,其中所有或至少部分盘形塔内部构件是如权利要求1所述的填料元件或由这类元件形成的。
10.一种从要求高分离效率的、高沸点的、对空气和/或温度敏感物质的混合物中得到纯物质的方法,是通过在中等真空下、在装有具有有序结构的金属织物填料的塔中进行精馏,其特征在于,在下述的塔中进行精馏
a)其中,液体分配是通过具有500个或更多滴液点/m2的通道式分配器进行,
b)其中,液体分配器的通道以相对于直接位于这些分配器下面的盘形塔内部构件的织物层成约90°的角安装,
c)其中,在液体分配器的下面安装两个或多个高度仅为20-100毫米的盘形塔内部构件,其中的织物层各以相互呈90°角扭转,
d)其中,所有或部分其余的盘形塔内部构件由权利要求1所述的填料元件形成,
e)其中,塔是这样设计的,以致在精馏期间通过塔壁不发生热交换,和
f)其中,对于空气敏感的物质,塔是这样设计的,以致它实际上是在隔绝空气下操作的。
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DE19524928.3 | 1995-07-08 | ||
DE19524928A DE19524928A1 (de) | 1995-07-08 | 1995-07-08 | Verfahren zur Rektifikation von Gemischen hochsiedender luft- und/oder temperaturempfindlicher Substanzen, die eine hohe Trennleistung erfordern, im Feinvakuum, sowie für dieses Verfahren geeignete Kolonnen |
DE1996105286 DE19605286A1 (de) | 1996-02-13 | 1996-02-13 | Druckverlustarme Gewebepackungen oder gewebeähnliche Packungen mit geordneter Struktur zur Verwendung in Stoffaustauschkolonnen |
DE19605286.6 | 1996-02-13 |
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CN1190356A true CN1190356A (zh) | 1998-08-12 |
CN1090055C CN1090055C (zh) | 2002-09-04 |
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US (1) | US5950454A (zh) |
EP (1) | EP0846027B1 (zh) |
JP (1) | JPH11508817A (zh) |
CN (1) | CN1090055C (zh) |
DE (1) | DE59603300D1 (zh) |
ES (1) | ES2138358T3 (zh) |
RU (1) | RU2193445C2 (zh) |
WO (1) | WO1997002890A1 (zh) |
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CN1121262C (zh) * | 1999-03-01 | 2003-09-17 | 永冈忠义 | 柱填充物及其制造方法 |
CN1121264C (zh) * | 1999-04-27 | 2003-09-17 | 永冈忠义 | 柱状填充物及其制造方法 |
CN100415359C (zh) * | 2003-05-16 | 2008-09-03 | 苏舍化学技术有限公司 | 金属织物制成的交叉通道填料的使用方法 |
CN100441286C (zh) * | 2005-04-28 | 2008-12-10 | 气体产品与化学公司 | 带有结构的填充物及其用途 |
CN111050870A (zh) * | 2017-06-20 | 2020-04-21 | 苏尔寿管理有限公司 | 分离装置的包括由碳复合材料制成的筛网的液体分配器 |
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DE19524928A1 (de) * | 1995-07-08 | 1997-01-09 | Basf Ag | Verfahren zur Rektifikation von Gemischen hochsiedender luft- und/oder temperaturempfindlicher Substanzen, die eine hohe Trennleistung erfordern, im Feinvakuum, sowie für dieses Verfahren geeignete Kolonnen |
EP0913192B1 (de) * | 1997-10-30 | 2003-04-16 | Sulzer Chemtech AG | Stoffaustauschkolonne mit einer Packung |
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DE19903459A1 (de) * | 1999-01-28 | 2000-08-03 | Basf Ag | Verfahren zur Herstellung von hochreinem Phytantriol |
DE19936380A1 (de) | 1999-08-03 | 2001-02-08 | Basf Ag | Geordnete Packung zum Wärme- und Stoffaustausch |
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DE10010810A1 (de) * | 2000-03-08 | 2001-09-13 | Montz Gmbh Julius | Flüssigkeitsverteiler und Verfahren zum Betreiben |
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DE102005001290A1 (de) * | 2005-01-11 | 2006-07-20 | Basf Ag | Vorrichtung und Verfahren zur Entfernung von Kohlenmonoxid aus einem wasserstoffhaltigen Gasstrom |
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- 1996-06-29 WO PCT/EP1996/002851 patent/WO1997002890A1/de active IP Right Grant
- 1996-06-29 CN CN96195315A patent/CN1090055C/zh not_active Expired - Fee Related
- 1996-06-29 US US08/973,875 patent/US5950454A/en not_active Expired - Fee Related
- 1996-06-29 RU RU98102152/12A patent/RU2193445C2/ru not_active IP Right Cessation
- 1996-06-29 EP EP96924819A patent/EP0846027B1/de not_active Expired - Lifetime
- 1996-06-29 ES ES96924819T patent/ES2138358T3/es not_active Expired - Lifetime
- 1996-06-29 JP JP9505459A patent/JPH11508817A/ja active Pending
- 1996-06-29 DE DE59603300T patent/DE59603300D1/de not_active Expired - Fee Related
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
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CN1121262C (zh) * | 1999-03-01 | 2003-09-17 | 永冈忠义 | 柱填充物及其制造方法 |
CN1121264C (zh) * | 1999-04-27 | 2003-09-17 | 永冈忠义 | 柱状填充物及其制造方法 |
CN100415359C (zh) * | 2003-05-16 | 2008-09-03 | 苏舍化学技术有限公司 | 金属织物制成的交叉通道填料的使用方法 |
CN100441286C (zh) * | 2005-04-28 | 2008-12-10 | 气体产品与化学公司 | 带有结构的填充物及其用途 |
CN111050870A (zh) * | 2017-06-20 | 2020-04-21 | 苏尔寿管理有限公司 | 分离装置的包括由碳复合材料制成的筛网的液体分配器 |
Also Published As
Publication number | Publication date |
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US5950454A (en) | 1999-09-14 |
ES2138358T3 (es) | 2000-01-01 |
JPH11508817A (ja) | 1999-08-03 |
DE59603300D1 (de) | 1999-11-11 |
EP0846027B1 (de) | 1999-10-06 |
CN1090055C (zh) | 2002-09-04 |
EP0846027A1 (de) | 1998-06-10 |
WO1997002890A1 (de) | 1997-01-30 |
RU2193445C2 (ru) | 2002-11-27 |
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