CN1543372A - 用于汽提和精镏流体混合物的装置 - Google Patents
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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- F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
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- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
- F28D2021/0066—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications with combined condensation and evaporation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2250/00—Arrangements for modifying the flow of the heat exchange media, e.g. flow guiding means; Particular flow patterns
- F28F2250/10—Particular pattern of flow of the heat exchange media
- F28F2250/104—Particular pattern of flow of the heat exchange media with parallel flow
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Abstract
一种热交换器在汽提段和精馏段之间使用。该热交换器(10)带有多个通道,所述通道在所有侧面上封闭,且具有用于相关段的端部入口和端部出口。压缩机安装在各段之间。根据本发明的热交换器是紧凑式热交换器,即热交换器由一系列的相邻板片(15,16)组成,在这些相邻板片之间,用于所述汽提段或精馏段且在所有侧面上封闭的多个通道(11,12)受到限制。这些通道(11,12)基本上竖直延伸,并构造成使得所有包含在其内部的液体能够流向相关段的底部。汽提段/精馏段的通道的过流横截面根据在其中所进行的工艺而改变。
Description
技术领域
本发明涉及一种用于汽提和精馏流体混合物的装置,其包括:带有用于汽提段和精馏段的多个通道的热交换器,所述通道在所有侧面上封闭,且具有端部入口和端部出口;一个安装在所述汽提段的入口和所述精馏段的入口之间的压缩机;所述热交换器由一系列的相邻板片组成,在这些相邻板片之间,用于所述汽提段或精馏段且在所有侧面上封闭的多个通道被交替限定,这些通道基本上竖直延伸,并且它们的结构使得所有包含在它们内部的液体能够流向所述汽提段或精馏段的底部。
背景技术
美国专利US5,592,832中公开了这种装置。在该篇文献中描述了被称为热集成蒸馏塔的工艺。在该工艺中,压缩机安装在汽提段和精馏段之间。此外,在汽提段和精馏段之间发生直接的热交换,也就是说在壳管式热交换器中存在从汽提段到精馏段的直接热交换。结果使得,冷凝器和再沸器可以制造得相对较小。这样,可以提高传统蒸馏的效率。如美国专利US5,592,832所描述的产生的压力偏差,与操作温度的相应偏差有关,结果使得热量能够直接从精馏段传递到汽提段。
这种装置用于例如分离沸点彼此接近的碳氢化合物,例如丙烷和丙烯。将这种混合物输送到汽提段的顶部;一方面,这种混合物下落穿过汽提段,另一方面,这种混合物被压缩机泵送到精馏段的入口处,该入口位于垂直布置的精馏段的底部。在各段中可选择使用填料。在操作过程中,在汽提段的顶部有相对多的气液流,而底部则气液流较少。对于精馏段来说,情况正好相反。即,在其底部具有较多的气液流,而在顶部则气液流较少。
这种结构使得有可能在汽提段中有效地利用来自精馏段的较高热量。这与现有工艺中较低的热量只在冷凝器中回收,而较高的热量只供给再沸器的过程相反。因此,该工艺的产量可以提高。
美国专利US5592832公开了一种带有两组用于汽提和精馏的通道的板翅式热交换器。该热交换器具有多个竖直延伸的彼此并排平行布置的板片/翅片。EP0726085A1也公开了一种热集成蒸馏塔(HIDiC)工艺。
发明内容
本发明的目的是提供一种装置,该装置具有可以以非常紧凑的方式实现的热交换器。这种紧凑的结构能够优化热量和质量的传递。
由于在上述装置中,所述各段的通道的过流横截面从入口端到出口端减小,所以通过该装置可以实现上述目的。
考虑到在各段中不同位置和不同状态下的气液流,根据本发明,将一段或两段的通道的过流横截面构造成从入口向出口变小。最终,气液流朝向出口减少,使得所需要的体积变小。通过使汽提段和精馏段的通道并排地布置,有可能最优化地利用板片之间的空间。但是,尽管使用了该结构,仍然有必要采取措施对各段彼此之间进行密封。
如果利用逆向流的原理,也就是说,在汽提段中出口位于入口下方,而在精馏段中出口位于入口上方;相邻的通道可以发生会聚,从而其轴线保持平行。
根据又一优选实施例,可以通过改变热交换器的两个相对壁之间的距离来改变相关通道的横截面。热交换器的其他壁(端部板片)彼此平行。
可以采用本技术领域中任何公知的方法来生产这种类型的紧凑式热交换器。根据一个优选实施例,通道凹入板片中,特别是利用蚀刻在板片中形成通道。此外,有可能在一个或多个板片中制出通道,并以本技术领域中公知的方法来将这些板片彼此连接起来。特别地,可以使用扩散接合的方法来达到此目的。
与壳管式热交换器相比,紧凑式热交换器的每单位体积的热交换面积更大。因此,所述紧凑式热交换器装置可以变得更加紧凑,且可以限制温度差异,这样又能够减少压力差异,进而能够使用更小更低廉的压缩机,同时增加产出。
根据本发明的又一优选实施例,有可能对上述的板片或添加的部件涂以例如催化剂材料,或者向有关的通道引入这样的催化剂材料或其他颗粒状的反应剂。
紧凑式热交换器可以制成模块化结构,这样,可以容易进行修改以适应条件的改变。此外,有可能通过调节紧凑式热交换器的几何形状来调节热传递表面面积和质量传递表面面积之间的比例,该比例对于良好的设计非常重要。这特别适用于上述的实施例,其中例如成波纹状延伸的翅片位于平行的板片之间。通过调节数量和/或间隔,可以影响热传递和质量传递之间的比例。
上述的装置可用于汽提/精馏多种物质。这些物质不限于碳氢化合物或丙烷/丙烯。
这种紧凑式热交换器可以以多种方式构建。总体上,每个竖直通道将在热交换表面上面设有一个液体入口和气体出口,在热交换表面下面设有一个气体入口和液体出口。此外,每个通道的这些入口和出口必须被布置成借助套管或歧管可以连接到其他通道的对应部分上。气液流之间的分离不必在每个的通道中都发生,只要在通道外边可以实现分离即可。进入的介质在多个通道上都均匀分布很重要,这样可以最优化热量交换和质量交换。如果合适的话,可以为达到此目的而采取特别的措施。这同时也适用于气体出口液体入口以及气体入口液体出口。
附图说明
本发明的更多细节将参照如下附图中的示例性实施例作出说明。在附图中:
图1显示热集成蒸馏塔概念的一般操作过程;
图2显示构成板翅式热交换器的紧凑式热交换器;
图3a和3b显示一个具体的紧凑式热交换器中通道的形状;
图4显示图2和3中所示构造的可替换方案。
具体实施方式
图1概略地显示了分离两种成分的方法。将要被分离的混合物从1处被输送到汽提段S。气态产物通过管线输送到压缩机2,并以一种没有具体显示的方式被压缩并输送到精馏段R。在该精馏段中产生的液态产物被返回到管线1。气体被输送到冷凝器3。
汽提段S中产生的液体被输送到再沸器4,然后作为底部产物部分排出。从精馏段到汽提段的热传递如箭头5表示。可以理解,使这种热传递尽可能高效率地进行是非常重要的。
根据本发明,可以由被称为紧凑式热交换器的装置来达到提高效率。
图2给出了这种热交换器的一个示例,图中用10表示一个紧凑式热交换器的整体。该热交换器包含交替通道11和12。在每个通道中分别具有以弯曲形式延伸的翅片13和14。这些翅片被安置为能够使这些通道总是垂直延伸。板片15和16总是分别位于通道11和12之间。
如图中清晰显示,每个通道的横截面积从底部到顶部是变化的。通道11是汽提段的一部分,其横截面积从底部向顶部增加。通道12是精馏段的一部分,其横截面积从底部向顶部减少。在这两种类型的通道中都具有气体向上流动和液体向下流动的逆向流。垂直于热传递板片15和16的通道的端部板片彼此平行。通道11和12可以设有诸如规整填料的可选填充物,来代替翅片,以改善传质过程。各种基于丝网、线网或波纹板而制造的规整填料,对于蒸馏领域的技术人员来说是熟知的。
此附图中没有包括歧管。
图3a和3b示出了板片24和25,它们彼此接触排列,并且内部分别加工有通道26和27。如图所示,这些通道具有会聚/扩散结构。图3a涉及汽提段,因为在这个位置会出现相对较少的气液流,所以其横截面沿着向底部方向减少。图3b显示了精馏段,其中通道的构造完全相反。除了锥形形状之外,通道也可以做成阶梯状或以其他方式改变横截面的形状。
这些通道可选地填充含有反应剂或催化剂的填料。
图4a和4b显示了改变通道横截面的变化型式。与图3相比,在这些附图中板片不是平行地安放。这优选是板翅式热交换器。
图4a中的板片彼此倾斜(如图2所示),而图4b中的板片是阶梯状结构。
虽然上文中参照紧凑式热交换器的几个实施例对本发明做出了描述,但是本领域技术人员可以理解更多的变化型式。可以参考由能源示范技术分析与发布中心(Center for the Analysis andDissemination of Demonstrated Energy Technologies)出版的、David Reay教授的《从实践中学习紧凑式热交换器》(Learningfrom experience with compact heat exchanger)中所描述的紧凑式热交换器。此外,还可以参考由J.E.Hesselgreaves于2001年在帕加马出版的《紧凑式热交换器》(Compact heatexchanger)。热交换器可以有很多不同的型式。这些变化型式都属于本发明的范围。两个平行板片被缠绕在一起且表现为螺旋结构的实施例,可以作为上述的本发明示例。压缩机可以依据工艺来设计。同样地,如图1所示,冷凝器3和/或再沸器4的尺寸以及样式也取决于工艺。
在阅读了上述说明之后,这些以及更多的变化型式对于本领域的技术人员是显而易见的,并且包含在后面所述的权利要求书的范围内。
Claims (10)
1、一种用于汽提和精馏流体混合物的装置,其包括:
带有用于汽提段和精馏段的多个通道的热交换器,所述通道在所有侧面上封闭,且具有端部入口和端部出口;
安装在所述汽提段入口和所述精馏段入口之间的压缩机;
所述热交换器由一系列的相邻板片组成,在这些相邻板片之间,用于所述汽提段或精馏段且在所有侧面上封闭的多个通道被交替限定,所述通道基本上竖直延伸,并且它们的结构使得所有包含在它们内部的液体能够流向所述汽提段或所述精馏段的底部,其特征在于:所述汽提段或精馏段的通道的过流横截面从入口端向出口端减小。
2、如权利要求1所述的装置,其中所述过流横截面逐渐变化。
3.如权利要求1或2所述的装置,其中所述过流横截面逐级减少。
4.如前面任一权利要求所述的装置,其中所述通道包括在板片中的凹槽。
6.如权利要求5所述的装置,其中所述通道是从所述板片中蚀刻而成。
7.如前面任一权利要求所述的装置,其中所述通道被彼此相邻放置的板片部分限定,所述板片部分通过扩散接合而彼此装配起来。
8.如前面任一权利要求所述的装置,其中所述精馏段的出口端连接到冷凝器。
9.如前面任一权利要求所述的装置,其中所述精馏段的出口端连接到再沸器。
10.如前面任一权利要求所述的装置,其中所述热交换器是逆向流热交换器,所述汽提段和所述精馏段的横截面从入口端到出口端减少。
11.如权利要求10所述的装置,其中所述汽提段通道的轴线平行于所述精馏段通道的轴线。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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NL1018672 | 2001-07-31 | ||
NL1018672A NL1018672C2 (nl) | 2001-07-31 | 2001-07-31 | Stelsel voor het strippen en rectificeren van een fluïdummengsel. |
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CN1543372A true CN1543372A (zh) | 2004-11-03 |
CN1275672C CN1275672C (zh) | 2006-09-20 |
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CNB028161777A Expired - Fee Related CN1275672C (zh) | 2001-07-31 | 2002-07-31 | 用于汽提和精馏流体混合物的装置 |
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US (1) | US7111673B2 (zh) |
EP (1) | EP1412044B1 (zh) |
JP (1) | JP4125674B2 (zh) |
CN (1) | CN1275672C (zh) |
AT (1) | ATE286772T1 (zh) |
DE (1) | DE60202611T2 (zh) |
ES (1) | ES2235063T3 (zh) |
NL (1) | NL1018672C2 (zh) |
WO (1) | WO2003011418A1 (zh) |
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-
2001
- 2001-07-31 NL NL1018672A patent/NL1018672C2/nl not_active IP Right Cessation
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2002
- 2002-07-31 WO PCT/NL2002/000517 patent/WO2003011418A1/en active IP Right Grant
- 2002-07-31 ES ES02747764T patent/ES2235063T3/es not_active Expired - Lifetime
- 2002-07-31 DE DE60202611T patent/DE60202611T2/de not_active Expired - Lifetime
- 2002-07-31 JP JP2003516648A patent/JP4125674B2/ja not_active Expired - Fee Related
- 2002-07-31 US US10/485,365 patent/US7111673B2/en not_active Expired - Fee Related
- 2002-07-31 EP EP02747764A patent/EP1412044B1/en not_active Expired - Lifetime
- 2002-07-31 CN CNB028161777A patent/CN1275672C/zh not_active Expired - Fee Related
- 2002-07-31 AT AT02747764T patent/ATE286772T1/de not_active IP Right Cessation
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100439838C (zh) * | 2006-09-08 | 2008-12-03 | 浙江大学 | 一种节能空分装置 |
CN102065995B (zh) * | 2008-06-30 | 2014-02-26 | 环球油品公司 | 改进的安装在塔内的冷凝器 |
CN103154654A (zh) * | 2010-09-23 | 2013-06-12 | 特诺恩股份公司 | 用于快速冷却炼铁厂烟气的热交换器、包括这种热交换器的用于处理炼铁厂烟气的设备以及相关处理方法 |
CN103154654B (zh) * | 2010-09-23 | 2016-02-24 | 特诺恩股份公司 | 用于快速冷却炼铁厂烟气的热交换器、设备以及方法 |
CN103379947A (zh) * | 2011-01-18 | 2013-10-30 | 荷兰能源建设基金中心 | 采用结构性热交换器的热集成蒸馏塔 |
CN103379948A (zh) * | 2011-01-18 | 2013-10-30 | 荷兰能源建设基金中心 | 采用规整填料的热集成蒸馏塔 |
CN106839832A (zh) * | 2017-01-23 | 2017-06-13 | 中国科学技术大学 | 一种用于超临界流体热力循环中的变流道换热器 |
CN110230935A (zh) * | 2019-06-12 | 2019-09-13 | 南京工业大学 | 一种柔性结构的强热适应性板翅式换热器芯体 |
Also Published As
Publication number | Publication date |
---|---|
DE60202611D1 (de) | 2005-02-17 |
JP4125674B2 (ja) | 2008-07-30 |
WO2003011418A1 (en) | 2003-02-13 |
EP1412044A1 (en) | 2004-04-28 |
US7111673B2 (en) | 2006-09-26 |
JP2004536701A (ja) | 2004-12-09 |
DE60202611T2 (de) | 2005-12-29 |
US20040200602A1 (en) | 2004-10-14 |
ES2235063T3 (es) | 2005-07-01 |
NL1018672C2 (nl) | 2003-02-06 |
EP1412044B1 (en) | 2005-01-12 |
ATE286772T1 (de) | 2005-01-15 |
CN1275672C (zh) | 2006-09-20 |
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