CN1904531B - 低温蒸馏分离空气的方法和装置 - Google Patents

低温蒸馏分离空气的方法和装置 Download PDF

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CN1904531B
CN1904531B CN 200610106497 CN200610106497A CN1904531B CN 1904531 B CN1904531 B CN 1904531B CN 200610106497 CN200610106497 CN 200610106497 CN 200610106497 A CN200610106497 A CN 200610106497A CN 1904531 B CN1904531 B CN 1904531B
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air
heat exchanger
stream
delivered
main heat
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CN1904531A (zh
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T·帕乌尔斯基
M·A·突尼
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
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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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    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

一种采用塔系统进行空气分离的低温蒸馏装置，包括至少一个塔(HP、LP、M)、一主热交换器(E1)、用于将冷却的压缩空气送至主热交换器、以及从主热交换器送到塔系统的管道、用于将富氧、富氮流从塔系统送至主热交换器的管道、清除流蒸发器(E2)、用于从塔系统排出清除流(31)并将该清除流送至清除流蒸发器的管道、用于将压缩和净化的空气(9)送至清除流蒸发器的管道、以及用于将压缩和净化的空气从清除流蒸发器送至塔系统的管道。

Description

低温蒸馏分离空气的方法和装置
技术领域
本发明涉及一种低温蒸馏分离空气的方法和装置。
背景技术
低温蒸馏空气分离单元包括将空气分馏成重组分和轻组分的蒸馏部分。在该工艺过程中，烃类物质会在液氧流中聚集，可造成安全隐患。前置的氧化铝和分子筛吸附床并不能阻止所有的这些杂质进入蒸馏过程中。
除去富氧液流中杂质残余物的传统方法包括通过硅胶床的额外吸附步骤。另一种可选的方法是仅排出一小部分含烃类物质的氧液流以防止重杂质的累积，从而使其浓度保持在一足够低的水平上。这种方法仅仅适用于那些小型工程，其中，相对于排出液氧导致的冷量损失，硅胶吸附单元的额外投资显得更高。因此，希望有一种有效节约成本的系统，它不仅能够除去危险的烃类物质，也不会由于排出液氧而导致大量的冷量损失。美国专利US5,379,599和US5,471,842公开了泵压输送一清除流并在主热交换器中对其进行汽化的情形。
发明内容
本发明为此提出了安装一个与主热交换器分离的小型清除流汽化热交换器，它可以回收清除液流的大部分冷量。该热交换器采用暖空气流来蒸发和加热氧气流。该热蒸发的氧气可以直接排出也可以与气态氧混合从主热交换器排出作为产品。该暖空气流可以来自于吸附床、增压压缩机、或其它的热压缩源的排出气。控制输送至该热交换器的空气流的流量，保持离开该热交换器的冷却空气的温度高于一设定值(～-90℃)，从而避免烃类物质沉积在交换器里面。
附图说明
为了进一步了解本发明的本质和目的，结合附图进行下列详细的说明，附图中相同或类似的附图标记代表类似的部件，其中：
-图1示出了采用并立双塔和一个混合塔制备氧气的本发明的空气分离单元；
-图2示出了采用单塔制备氮气的本发明的空气分离单元。
具体实施方式
在图1中，低压塔LP设置在同一结构中的混合塔M的上方，高压塔HP分开设置但是经由冷凝器C与低压塔热连接。
将基本上处于高压塔HP压力的经压缩和净化的空气流1输送到冷箱。将其分为三股流体。第一股流体3不经过冷却直接送至增压压缩机B，在那里被压缩，使其压力明显高于高压塔的压力，然后将其分成9和11两部分。流体9被送至热交换器E2，而流体11先在后冷却器A中被冷却，然后进一步被送至主热交换器E1进一步冷却。
热交换器E2可以是管壳式、螺旋管式或其它可以处理大温度差、并能避免交换器通道可能的堵塞的任何类型。
空气流9用于在热交换器E2中使从高压塔冷凝器出来的清除氧气流31汽化。进入热交换器E2的空气的温度高于环境温度，而该氧气流是在低温下被泵送。为了防止烃类物质沉积在热交换器E2中，有必要调节空气流9，从而使得离开热交换器E2的空气的温度高于一设定值(～-90℃)。例如，可以在交换器E2的空气出口处放置一个温度检测和控制器(TIC)，用其来控制阀门V，调节空气流9。
流体11被冷却至热交换器E1的中温，并与来自交换器E2的冷却空气流9一起送至汽轮膨胀机T。然后将膨胀后的空气流13送至低压塔LP。
空气流5被冷却至热交换器E1的中温，然后送至混合塔M的底部。
空气流7从热交换器E1的较高温度端流向低温端，然后被送至高压塔HP的底部。
所示的塔包括一种常规设置的混合塔，其中液氧29从冷凝器被送至混合塔M的顶部，液氮21从高压塔HP被送至低压塔LP的顶部，富氧液体23从高压塔的底部被送至低压塔。混合塔M的中间液体17和底部液体15被输送到低压塔LP。底部液体15在进入塔LP前优选与空气流13混合。
向冷凝器C供入来自LP塔的底部液体25，产生蒸发的气态氧气27，该氧气27被送回低压塔。
气态氮气19从低压塔的顶部排出，并在热交换器E1中被加热。
来自混合塔M顶部的气态氧气33被输送到热交换器E1中，加热至较高温度端，并与来自热交换器E2的被蒸发的氧气31混合，形成产物氧气流35。
空气流在返回工艺过程前通过清除流蒸发器E2、控制阀V和管道时具有足够的压降很重要。如果获得的压降太低，可能无法实现使足够的空气流通过清除流蒸发器，以至不能正常工作。另一方面，如果采用过大的压降(例如采用中压空气并经汽轮机后返回低压回路)，则汽轮机中流速的降低将会导致冷量损失，从而降低了清除流蒸发器的冷量获益。
如果空气来自增压压缩机的后冷却器之前的排出气，该空气可以被回注到汽轮机的入口，这样冷量不会损失(参见附图1)。这种情况下，空气流绕过后冷却器和主热交换器的较高温部分。这样可对清除流蒸发器和控制阀门产生足够的压降，因为增压器后冷却器通常明显吸收压降。
如果空气流取自增压压缩机(如果有的话)的上游，该空气流一般返回到主热交换器低温端的空气流中。这种情况下，汽化的清除流流体回送到废氧气膨胀器的入口以使冷量的损失最小化。
图2的空气分离单元采用了一个具有塔顶双再沸器的单一塔。在图2中，压缩的纯化空气流1被分成两个部分，形成空气流9和空气流5。空气流5被送至热交换器E1，在那里被冷却，然后被送至塔HP的底部。空气流9被送至热交换器E2，不经过热交换器E1。之后，空气流9与冷却后的空气流5混合，送至塔HP。
来自塔底部的富氧液体15在热交换器E3中被继续冷却后，送至冷凝器C1。冷凝器C1用于在塔顶部冷凝部分气态氮，从而蒸发部分富氧液体。蒸发的富氧液体被送至增压器B中，并在低于流体5的塔入口点之处回到塔中。
未在C1中蒸发的富氧液体被送至冷凝器C2，冷凝器C2位于冷凝器C1的下方。冷凝器C2同样也是用来在塔顶部冷凝部分气态氮，由此蒸发部分剩余富氧液体。未在C2中蒸发的富氧液体作为清除流31排出，在热交换器E2中用空气流9汽化。汽化的清除流在汽轮机T中膨胀，驱动增压机B，用于在热交换器E3中冷却富氧液体，在热交换器E1中被加热，然后作为流体53从系统中排出。
产物氮气33从塔的顶部排出，在热交换器E1中被加热。中间纯度的氮气19从塔的中部排出，在热交换器E1中被加热。液态氮气51从塔的顶部排出，送至储存罐S。
很明显，本发明也可以用于其它类型的空气分离单元，例如单塔单元、双塔单元和附加其它塔诸如氩气塔的双塔单元，以及三塔单元。总的来说，本发明可以用于任何需要清除重组分和回收冷量和/或清除流分子的装置。清除流取自蒸发器或塔的底槽，其中含有最高浓度的重组分(烃类等)。本发明的必要技术特征在前面公开的内容中进行了充分的描述。本领域技术人员可以理解本发明，并在不脱离本发明实质、不偏离后面权利要求书和其等同物的范围的情况下作出各种改变。

Claims (10)

1.一种采用包括至少一个塔的塔系统的低温蒸馏空气分离方法，包括以下步骤：
a)在一压缩机里压缩进料空气以产生压缩空气；
b)在一净化单元中净化压缩的空气以产生压缩和净化的空气；
c)将压缩和净化的空气送至一主热交换器以产生冷却的、压缩和净化的空气；
d)将冷却的、压缩和净化的空气送至塔系统；
e)从该塔系统中排出富氮和富氧流，并在主热交换器中加热该富氮和富氧流；
f)从该塔系统中排出液态清除流；和
g)该液态清除流不经过主热交换器加热，通过与温度高于0℃的流体的热交换汽化该液态清除流。
2.根据权利要求1所述的方法，其中该温度高于0℃的流体为空气流。
3.根据权利要求2所述的方法，其中该空气流来自压缩器的下游。
4.根据权利要求3所述的方法，其中该空气流来自净化单元的下游。
5.根据权利要求4所述的方法，其中该空气流来自增压压缩器的下游。
6.根据权利要求1所述的方法，其中所述液态清除流在一与主热交换器分离的另一热交换器中汽化。
7.根据权利要求6所述的方法，其中控制输送至所述另一热交换器的空气流的流量，保持离开该热交换器的冷却空气的温度高于一设定值。
8.一种采用包括至少一个塔的塔系统进行空气分离的低温蒸馏装置，其还包括以下设备：
a)一主热交换器；
b)用于将冷却的压缩空气送至主热交换器、以及从立热交换器送至塔系统的管道；
c)用于将富氧和富氮流从塔系统送至主热交换器的管道；
d)一清除流蒸发器；
e)用于从塔系统排出清除流并将该清除流送至清除流蒸发器的管道；
f)用于将压缩和净化的空气送至清除流蒸发器的管道；以及
g)用于将压缩和净化的空气从清除流蒸发器送至塔系统的管道。
9.根据权利要求8所述的装置，其中清除流蒸发器是螺旋型热交换器或管壳式热交换器。
10.根据权利要求8所述的装置，其中主热交换器是板翅式热交换器。
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