CN1769196A - 折返式电除盐器 - Google Patents

折返式电除盐器 Download PDF

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CN1769196A
CN1769196A CNA2004100678571A CN200410067857A CN1769196A CN 1769196 A CN1769196 A CN 1769196A CN A2004100678571 A CNA2004100678571 A CN A2004100678571A CN 200410067857 A CN200410067857 A CN 200410067857A CN 1769196 A CN1769196 A CN 1769196A
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李翔
仝志明
潘鸿舞
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OKUMEI ENVIRONMENT ENGINEERING Co Ltd ZHEJIANG
Zhejiang Omex Environmental Engineering Co Ltd
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OKUMEI ENVIRONMENT ENGINEERING Co Ltd ZHEJIANG
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Priority to JP2007538250A priority patent/JP4709224B2/ja
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Priority to US11/666,824 priority patent/US8173003B2/en
Priority to PCT/CN2005/001822 priority patent/WO2006047945A1/zh
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Abstract

本发明涉及一种电除盐器，尤其涉及一种折返式电除盐器。包括作为电极一极的中心管和与其同心外壳，外壳上设有电极的另一极，在中心管和外壳间设置有交替布置的阴阳离子交换膜，以中心管为中心，将上述若干层的阴阳离子交换膜和浓淡水通道内的网隔板，淡水通道内的阴阳离子交换树脂制成圆柱体，所述的淡水通道分为内、外两个流水通道单元。本发明主要是解决现有技术所存在的电除盐器装置各个断面上电流密度分布差异较大，造成产水水质不稳定，且装置的制造成本较高等技术问题；提供了一种结构合理，装置中各断面电流密度分布较为均匀，产水水质较为稳定，经济性较好的折返式电除盐器。

Description

折返式电除盐器
技术领域
本发明涉及一种电除盐器，尤其涉及一种折返式电除盐器。
背景技术
现有工业用水除盐提纯的水处理的方法中，较为先进的方法是将电渗析技术和离子交换技术相结合来制取超纯水，即电除盐(EDI)。例如，有人申请了专利：螺旋卷式电除盐器(98223514.3)，它提供了一种螺旋卷式的电除盐器的水处理设备，它主要将阴阳离子交换膜与绝缘网隔板制成一特殊的膜袋式浓水流道单元，并与浓水配集管的侧壁相连通，每相邻的浓水流道单元之间夹入一张绝缘网隔板构成可充填入离子交换树脂的淡水流道单元，然后以浓水配集管为中心卷绕成圆柱体结构，再包以金属壳体。该实用新型具有结构简单，流道阻力小、更换离子交换树脂方便等优点，但是此种结构存在电流密度分布不均匀，从而导致外围的脱盐能力最差，越往中心越好，使得在装置的各个断面上，形成性能差异。还有美国专利US6376253提供了一种螺旋卷式结构的电除盐装置，采用径向进水方式，被处理水从外圆呈螺旋状流向中心，这种设计虽然较好的解决了内外电流密度差的问题，但是为了保证装置的产水量，只能采取增加轴向长度，从而增加了电极的长度，提高了装置的制造成本，同时制造工艺复杂。
发明内容
本发明主要是解决现有技术所存在的电除盐器装置各个断面上电流密度分布差异较大，造成产水水质不稳定，且装置的制造成本较高等技术问题；提供了一种结构合理，装置中各断面电流密度分布较为均匀，产水水质较为稳定，经济性较好的折返式电除盐器。
本发明的上述技术问题主要是通过下述技术方案得以解决的：一种折返式电除盐器，包括作为电极一极的中心管和与其同心外壳，外壳上设有电极的另一极，在中心管和外壳间设置有交替布置的阴阳离子交换膜，以中心管为中心，将上述若干层的阴阳离子交换膜和浓淡水通道内的网隔板，淡水通道内的阴阳离子交换树脂制成圆柱体，所述的淡水通道分为内、外两个流水通道单元。其中电极的阴阳两极是中心管和外壳，也可以是中心管和设置在外壳上的电极，两电极设有直流电源；内外两个流水通道单元，使得淡水的流程为折返式的，从而克服了电流密度不均造成的产水质量不高的问题，而且折返式的设计，在保证一定的产水量的情况下，缩短了轴向的长度，节约了阴阳电极及交换装置材料，降低了生产的成本。
作为优选，所述的折返式电除盐器为螺旋卷式结构，即阴阳离子交换膜和浓水通道内的网隔板，淡水通道内的阴阳离子交换树脂呈螺旋卷式状布置。
作为优选，所述的折返式电除盐器为同心圆结构，即阴阳离子交换膜和浓水通道内的网隔板，淡水通道内的阴阳离子交换树脂呈同心圈状布置。
作为优选，所述的淡水通道的内、外两个流水通道单元一端平齐，另一端呈阶梯状，在内、外淡水通道单元间，有阶梯状的一端设有内圈。内、外两个流水通道单元的阶梯状的设置使得流道通畅，液体流动阻力更小。
作为优选，所述的淡水通道是由阴阳离子交换膜与阴阳离子交换树脂构成，其内、外两个流水通道单元是将阴阳离子交换膜的中间粘合形成的，内、外两个流水通道单元的淡水膜面积之比为1∶0.8-1∶3，淡水室的宽度3-8mm。
作为优选，所述的中心管外径与外流水通道单元的外直径之比为1∶1.5-1∶2.5。
作为优选，所述的中心管为工程塑料管，其表面复合薄板，采用电极柱将其固定。薄板可以是钛涂钌薄板，也可以是钛涂铂薄板，还可以是铂薄板，但是以钛涂钌薄板为优，因为其更加经济实惠。当然，本优选方案并不排除中心管采用金属管或其他材料制成的结构。
作为优选，电除盐器的有效脱盐部分的高度与外缘直径之比为1∶0.7-1∶2。从而节约了成本，经济性价比更高。
作为优选，所述的内、外两个流水通道单元的淡水侧的膜面积之比为1∶0.85-1∶1.5。
因此，本发明具有根据原水流经电除盐器各个断面时的实际脱盐情况，充分利用了电除盐器内外侧电流密度不同的特点，具有结构合理，布置科学，水流阻力较小，实现原水的深度脱盐，尤其是弱电解质的脱除大大提高，提高了产水的质量等优点。
同时克服了原有技术中心区域过电流的技术问题，降低了电耗，节省了装置的制造成本。
附图说明：
附图1是折返式电除盐器的整体视图。
附图2是折返式电除盐器的浓淡水通道的剖视图。
附图3是折返式电除盐器的横截面结构示意图。
具体实施事例：
下面通过实施例，并结合附图，对本发明的技术方案作进一步具体的说明。
实施例1：如附图1或2所示，折返式电除盐器以中心管1为轴心，中心管1为工程塑料管，表面复合钛涂钌薄板，用电极柱7将其固定作为电除盐器的阳电极，外壳作为阴电极，两电极设置有直流电源；在中心管1外有布置有若干个浓、淡水流道，浓、淡水通道间均设有的网隔板4和阴阳离子交换膜3，淡水通道内还填充有离子交换树脂，以中心管1为轴心，将其呈螺旋状卷制成个圆柱体。浓水通道是将上下两端封闭，左右两侧设有开口，浓水从浓水室外侧一端的浓水入口流入，在浓水室靠近中心管1上端设有一开口流出；淡水通道靠近中心管1的内侧和靠近外壳2的两端封闭，而上下两端为进水口和出水口，在淡水通道中间处将阴阳离子交换膜3粘合，形成内、外两个流水通道单元5，内、外两个流水通道单元的淡水膜面积之比为1∶0.85。内、外两个流水通道单元5的下端平齐，上端形成阶梯状，内侧的流水通道单元上端面高于外侧流水通道的上端面，原水自装置外端，淡水室外侧的流水通道单元上端面进入，沿轴向流经外围流水通道的各个断面，透过淡水室下端的集水板，转入装置的内侧的流水通道单元，同样流经内侧流水通道的各个断面，折返至装置内侧的出水端(如附图2所示)，形成一个折返式的流水通道，淡水室的宽度为6mm，由此种设计大大缩小了装置外圈部分与中心部分各自不同部位的电流密度差，原水由外侧折返至到内侧，使得原水的流道在流经相同的长度，保证一定产水量的情况下，装置的体积变小。在内、外两个流水通道单元5的上端设有内圈6，在外壳2的上下两端的侧面都设有浓、淡水的进水口通道8。其中，外侧流水通道单元的直径为Φ350mm，内侧流水通道单元的直径为Φ280mm，中心管直径为Φ160mm，整个电除盐器外径为Φ400mm，高度为Φ430mm。
实施例2：上述的结构的折返式电除盐器，以中心管为中心，若干层阴阳离子交换膜和设于浓、淡水通道内的网隔板为同心圆结构的圆柱体，其余部分结构和上述相同。外侧流水通道单元的直径为Φ400mm，内侧流水通道单元的直径为Φ340mm中心管直径为Φ250mm整个电除盐器的外缘直径Φ440mm，高度为Φ450mm，淡水室的宽度为6mm。其他结构不详部分参见实施例1。

Claims (11)

1.一种折返式电除盐器，包括作为电极一极的中心管(1)和与其同心外壳(2)，外壳(2)上设有电极的另一极，在中心管(1)和外壳(2)间设置有交替布置的阴阳离子交换膜，以中心管(1)为中心，将上述若干层的阴阳离子交换膜(3)和浓淡水通道内的网隔板(4)，淡水通道内的阴阳离子交换树脂制成圆柱体，其特征在于：所述的淡水通道分为内、外两个流水通道单元(5)。
2.根据权利要求1所述的折返式电除盐器，其特征在于：折返式电除盐器为螺旋卷式结构。
3.根据权利要求1所述的折返式电除盐器，其特征在于：折返式电除盐器为同心圆结构。
4.根据权利要求1或2所述的折返式电除盐器，其特征在于：所述的淡水通道的内、外两个流水通道单元(5)一端平齐，另一端呈阶梯状，在内、外淡水通道单元(5)间，有阶梯状的一端设有内圈(6)。
5.根据权利要求1或2所述的折返式电除盐器，其特征在于：所述的淡水通道是由阴阳离子交换膜(3)与阴阳离子交换树脂构成，其内、外两个流水通道单元(5)是将阴阳离子交换膜(3)的中间粘合形成的，内、外两个流水通道单元(5)的淡水膜面积之比为1∶0.8-1∶3，淡水室的宽度为3-8mm。
6.根据权利要求4所述的折返式电除盐器，其特征在于：所述的淡水通道是由阴阳离子交换膜(3)与阴阳离子交换树脂构成，其内、外两个流水通道单元(5)是将阴阳离子交换膜(3)的中间粘合形成的，内、外两个流水通道单元(5)的淡水膜面积之比为1∶0.8-1∶3，淡水室的宽度为3-8mm。
7.根据权利要求1或2或3所述的折返式电除盐器，其特征在于：所述的中心管(1)外径与外流水通道单元的外直径之比为1∶1.5-1∶2.5。
8.根据权利要求6所述的折返式电除盐器，其特征在于：所述的中心管(1)外径与外流水通道单元的外直径之比为1∶1.5-1∶2.5。
9.根据权利要求1或2或3所述的折返式电除盐器，其特征在于：所述的中心管(1)为工程塑料管，其表面复合薄板，采用电极柱(7)将其固定。
10.根据权利要求1或2或3所述的折返式电除盐器，其特征在于：电除盐器的有效脱盐部分的高度与外缘直径之比为1∶0.7-1∶2。
11.根据权利要求6所述的折返式电除盐器，其特征在于：所述的内、外两个流水通道单元(5)的淡水侧的膜面积之比为1∶0.85-1∶1.5。
CNB2004100678571A 2004-11-02 2004-11-02 折返式电除盐器 Expired - Lifetime CN100518905C (zh)

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US11/666,824 US8173003B2 (en) 2004-11-02 2005-11-02 Turn-back flow EDI
PCT/CN2005/001822 WO2006047945A1 (fr) 2004-11-02 2005-11-02 Echange de documents informatises de flux de retour
CA002585036A CA2585036A1 (en) 2004-11-02 2005-11-02 A turn-back flow edi
ZA200703520A ZA200703520B (en) 2004-11-02 2005-11-02 A turn-back flow EDI
JP2007538250A JP4709224B2 (ja) 2004-11-02 2005-11-02 折り返しフロー型のｅｄｉ
EP05802027A EP1820564B1 (en) 2004-11-02 2005-11-02 Electrodeionisation apparatus with turn-back flow
AT05802027T ATE483515T1 (de) 2004-11-02 2005-11-02 Apparat zur elektrodeionisierung mit strömungsumlenkung
DE602005024040T DE602005024040D1 (de) 2004-11-02 2005-11-02 Apparat zur elektrodeionisierung mit strömungsumlenkung

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ZA200703520B (en) 2009-04-29
US8173003B2 (en) 2012-05-08
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CN100518905C (zh) 2009-07-29
AU2005300953A1 (en) 2006-05-11
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ATE483515T1 (de) 2010-10-15
WO2006047945A1 (fr) 2006-05-11

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