CN110678710B - 用于通过低温蒸馏分离空气的方法和设备 - Google Patents

用于通过低温蒸馏分离空气的方法和设备 Download PDF

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CN110678710B
CN110678710B CN201880033702.6A CN201880033702A CN110678710B CN 110678710 B CN110678710 B CN 110678710B CN 201880033702 A CN201880033702 A CN 201880033702A CN 110678710 B CN110678710 B CN 110678710B
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air
column
pressure
compressor
liquid
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CN110678710A (zh
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让-皮埃尔·特拉尼耶
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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
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
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    • F25J1/0015—Nitrogen
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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Abstract

披露了一种用于在塔系统中通过低温蒸馏分离空气的方法，该塔系统包括第一塔(8)和在比该第一塔低的压力下操作的第二塔(9)，该方法包括以下步骤：在第一压缩机(6)中将所有进料空气压缩至比该第一塔的压力大至少1巴的第一输出压力，将在该第一输出压力下的第一部分空气送至第二压缩机(230)，并且将空气压缩至第二输出压力，在热交换器(5)中冷却并冷凝在该第二输出压力下的至少部分空气，从该塔系统的塔中取出液体(OL)，加压液体(37)并在该热交换器(5)中通过热交换将液体汽化，并且将部分经压缩的空气减压至第二输出压力，在该热交换器中至少部分地汽化所述空气(107)，任选地在该热交换器中附加地加热所述空气，并且将至少部分的此空气送至第二压缩机(108)。

Description

用于通过低温蒸馏分离空气的方法和设备
本发明涉及用于通过低温蒸馏分离空气的方法和设备。本发明尤其涉及用于在升高的压力下生产氧和/或氮的方法和设备。
通过空气分离单元生产的氧气通常处于约20至50巴的高压。基本的蒸馏方案通常是在第二塔的底部生产氧的双塔工艺，其是在1至4巴的压力下进行。必须凭借氧气压缩机或凭借液体泵压工艺将氧压缩至较高的压力。由于与氧气压缩机有关的安全问题，最近的氧生产单元使用液体泵压工艺。为了使高压液氧汽化，需要附加的增压器，以便使部分进料氮或空气升高至较高的压力(在从40至80巴的范围内)。实质上，增压器代替了氧气压缩机。开发新工艺循环的目标之一是减小氧生产单元的能量消耗。
在减小此能量消耗的尝试中，可取的是在接近塔在引入进料空气流的点处的温度的温度下将所有进料空气流引入塔中，以便减小系统的热力学不可逆性。不幸的是，这使用“常规”泵送循环无法实现。
此现有技术在图1中示出。在图1中，如在FR-A-2 777 641中描述的，在空气分离单元1中使用双塔2，该双塔包括第一塔8和第二塔9(在比第一塔低的压力下操作)，这些塔通过再沸器/冷凝器10而热连接。将所有进料空气在压缩机6中压缩至第一塔8的压力，在纯化单元7中纯化并且再分成三份。
将流502送至增压器503中，在水冷却器(未呈现)中冷却，并且在热交换器5中进一步冷却，然后在耦接至增压器503的涡轮机501中减压。将经减压的空气502送至第二塔。
将另一部分空气送至基本上在与第一塔8相同的压力下的热交换器5。
将第三个流在压缩机230中压缩并且送至热交换器，在该热交换器中该流冷凝。将液化的空气在第一塔8与第二塔9之间进行再分。
使富含氧的液体流LR减压并且从第一塔送至第二塔。使富含氮的液体流LP减压并且从第一塔送至第二塔。通过第一塔生产纯液氮NLMP，然后在热交换器24中再次冷却，在阀143中减压，并且送至储存罐144。在第一塔的顶部取出高压氮气39，并且在热交换器中加热，以形成产物流40。从第二塔9的底部取出液氧OL，通过泵37加压并且以流38的形式部分地送至热交换器5，在该热交换器中将其通过与加压的空气进行热交换而汽化，以形成加压的氧气。剩余的液氧52以液体产物的形式取出。从第二塔9中取出富含氮的顶部气体流NR，并且以流33的形式在热交换器5中加热。
通过使用非纯氩塔3和纯氩塔4生产氩。非纯氩塔进料有源自第二塔9的流16。将液体流17从非纯氩塔3的底部送至第二塔9。将富层通过阀26送至塔3的顶部冷凝器12，并且将该层汽化以形成流27，将该流送回至第二塔。将产物流19送至冷凝器20，并且由此处形成流19。流19在热交换器20中冷凝，并且再分为流48(该流在交叉点50处被送至废物流33)以及另一个流。将另一个流通过阀21送至塔4。
纯氩塔4产生产物流45。纯氩塔4的顶部冷凝器13通过阀34进料有源自第一塔的富含氮的液体LP，并且通过阀35以流33的形式取出汽化的氮，并且在再冷却器24中冷却。
通过使用空气对纯氩塔的底部再沸器14进行加热，并且将液化的空气23送至第一塔。
还从中取出吹扫流46。
冷凝器20通过阀31进料有富含氮的液体LP，并且将汽化的液体通过阀32送至废物流33。
图2示出在交换器5中以kcal/h计的热交换与用于冷却和再加热流体的温度之间的关系。
现有技术中还描述了冷压缩方法的一些不同版本，如在US-A-5 379598、US-A-5475 980、US-A-5 596 885、US-A-5 901 576和US-A-6 626 008中。
在US-A-5 379 598中，通过增压器、随后通过冷压缩机将部分的进料空气再压缩，以提供汽化氧所必需的加压的流。此途径仍具有至少两个压缩机，并且纯化单元仍在低压下操作。
例如在US-A-5 475 980中描述的冷压缩方法提供了一种用于使用单个空气压缩机来控制氧生产单元的技术。在此方法中，将待蒸馏的空气在热交换器中冷却，然后通过由减压装置控制的增压器进行再次压缩，将其流出物送至双塔工艺的第一塔中，该塔在最高压力下操作。
这样做，空气压缩机的输送压力约为15巴，这同样非常有利于纯化单元。此途径的一个缺点在于由于附加的流再循环而导致热交换器的尺寸增加，这对于冷压缩单元是代表性的。可以通过增大交换器的温差来减小热交换器的尺寸。然而，这将导致不能有效使用能量，并且导致压缩机的输送压力较高，这将增加成本。
在US-A-5 596 885中，在热增压器中使部分进料空气经受更强力的压缩，在此期间至少部分空气在冷增压器中被进一步压缩。将源自这两个增压器的空气液化，并且在克劳德(Claude)涡轮机中将部分冷的经压缩的空气减压。
US-A-5 901 576描述了冷压缩方案的不同布置，其利用来自第一塔底部的汽化的富液体的减压或高压氮的减压以便驱动冷压缩机。在一些情况中还使用通过马达驱动的冷压缩机。这些方法还使用约在第一塔的压力下的进料空气来操作，并且在大多数情况下还需要增压器。
US-A-6 626 008描述了使用冷压缩机的热泵循环以改进用于生产双汽化器氧生产工艺用的低纯度氧的蒸馏方法。对于此类型的方法，低的空气压力和增压器也是代表性的。
EP-A-1 972 872描述了用于改进以上方法的器件，其依赖于冷压缩机，特别是通过在接近塔在引入进料空气流的点处的温度的温度下将所有进料空气流引入塔中，目的是为了减小系统的热力学不可逆性。然而，其需要增加至少一个附加的压缩级。
因此，本发明的目的在于克服这些方法的缺点，特别是通过在接近塔在引入进料空气流的点处的温度的温度下将所有进料空气流引入塔中，目的是为了减小系统的热力学不可逆性，而不增加附加的压缩级。因此，可以减少氧生产单元的产物的总成本。主要的改进是因为使用了增压空气压缩机(BAC)，以便一旦空气已经被使用就将其再循环，以便回收通过在主热交换器中高压液体汽化而产生的热量。
所提及的所有百分比都是摩尔百分比。
从US6336345中已知根据权利要求1的前序部分所述的方法。
根据本发明，提供了一种用于在塔系统中通过低温蒸馏分离空气的方法，该塔系统包括第一塔和在比第一塔低的压力下操作的第二塔，该方法包括以下步骤：
i)在第一压缩机中将所有进料空气压缩直至比该第一塔的压力大至多一巴、优选地基本上等于该第一塔的压力的第一出口压力，
ii)将在该第一出口压力下的第一部分的空气送至第二压缩机，并且将该空气压缩至第二出口压力，
iii)在热交换器中将在该第二出口压力下的至少部分空气冷却并冷凝，
iv)从该塔系统的塔中取出液体，将液体加压并且在该热交换器中通过热交换将液体汽化，
v)将在该第二出口压力下的经冷却并冷凝的至少部分空气减压至在该第一出口压力与该第二出口压力之间的中间压力，在该热交换器中至少部分汽化所述空气，任选地在该热交换器中加热所述空气，其特征在于，将至少部分的此空气送至该第二压缩机，以便将其压缩直至该第二出口压力。
将经纯化并冷却的空气从该第一压缩机送至该塔系统，以便在该塔系统中将其分离。
根据本发明的可以彼此组合的其他任选的方面：
-该减压在至少一个阀中进行，
-该减压在至少一个涡轮机中进行，并且产生功，
-在减压前的该至少部分的温度小于该液体的汽化温度和该热交换器中最小温差的总和，
-该第二压缩机是多级压缩机，
-所述至少第三压力至少为该第二压缩机的级之一的入口压力，
-该第二压缩机的级是由用于对该方法的流体减压的装置驱动，
-用于减压的装置的入口温度小于环境温度，
-该第二压缩机的至少一个级具有小于环境温度的吸入温度，
-该吸入温度大于该液体的汽化温度，但是与该汽化温度接近，
-该液体是富含氧的流，
-该液体是富含氮的流，
-一种或多种液体产物的生产流不大于进料空气的10％、优选地不大于进料空气的5％。
根据本发明的另一方面，提供了一种用于在塔系统中通过低温蒸馏分离空气的设备，该塔系统包括第一塔和在比该第一塔低的压力下操作的第二塔，该设备附加地包括：
i)第一压缩机，其用于将进料空气压缩直至比该第一塔的压力大至少一巴、优选地基本上等于该第一塔的压力的第一出口压力，
ii)第二压缩机，以及用于将在该第一出口压力下的第一部分的空气送至该第二压缩机的器件，以便将该空气压缩直至第二出口压力，
iii)热交换器，其中在该第二出口压力下的至少部分空气被冷却并冷凝，
iv)用于从该塔系统的塔中取出液体的器件、用于加压液体的器件、用于将经加压的液体送至该热交换器的器件、以及用于从该热交换器中取出经汽化的液体的器件，
v)用于减压在该第二出口压力下的经冷却并冷凝的部分空气的器件、用于将所述空气流体送至该热交换器的器件、用于将在至少第三压力(在该第一出口压力与第二出口压力之间的中间压力)下的已经在该热交换器中被汽化的至少部分所述空气送至该第二压缩机以便将其压缩直至该第二出口压力的器件，以及
vi)用于将经纯化并冷却的空气送至该塔系统以便在该塔系统中进行分离的器件。
根据本发明的其他任选的方面：
-第一储存罐和任选的第二储存罐独立于该塔系统，
-该设备包括用于减压在第二压缩机中压缩的部分辅助流的涡轮机。
现将参考以下图更详细地描述本发明：图3、5和6，这些图是代表根据本发明的用于低温分离空气的方法的流体循环方案，以及图4，其是图3的交换器5的热交换图表。
在图3的实施例中，在空气分离单元1中，使用双塔2，其包括可用的第一塔8和第二塔9，这两个塔通过再沸器/冷凝器10热连接。在压缩机6中，将所有进料空气压缩至比第一塔8的压力大至少一巴、优选地基本上等于第一塔8的压力的压力，使得在中间管道中的压力下降成为可能，将进料空气在纯化单元7中纯化并且再分成三份。
将流502送至增压器503中，在水冷却器(未呈现)中冷却，然后在热交换器5中再一次冷却，然后在耦接至增压器503的涡轮机501中减压。将经减压的空气502送至第二塔。
将另一部分空气507送至在基本上与第一塔8的压力相等的压力下的热交换器5。
将第三个流505在压缩机230中压缩并且送至热交换器，在该热交换器中该流冷凝。在这种情况下，认为压缩机230是离心式压缩机，其包括四级：230A、230B、230C和230D，例如为整体齿轮式，通过水中间冷却器232A、232B、232C以及后冷却器232D冷却。压缩机的吸入压力为5.5绝对巴，中间压力为10.2绝对巴、18.9绝对巴和35.1绝对巴，并且最终出口压力为65绝对巴。吸入流为总空气流的26.5％。在第一塔8、第二塔9与将在阀116A、116B和116C中减压的部分之间再分液化的空气。
使富含氧的液体流LR减压并且从第一塔送至第二塔。使富含氮的液体流LP减压并且从第一塔送至第二塔。
通过第一塔8生产纯液氮NLMP，在热交换器24中再次冷却，在阀143中减压，并且送至储存罐144。在第一塔的顶部取出高压氮气39，并且在热交换器中加热，以形成产物流40。从第二塔9的底部取出液氧OL，通过泵37加压并且以流38的形式部分地送至热交换器5，在该热交换器中将其通过与加压的空气进行热交换而汽化，以形成加压的氧气。剩余的液氧52以液体产物的形式取出。从第二塔9中取出富含氮的顶部气体流NR，并且以流33的形式在热交换器5中加热。
通过使用非纯氩塔3和纯氩塔4生产氩。非纯氩塔进料有源自第二塔9的流16。将液体流17从非纯氩塔3的底部送至第二塔9。将富含氧的液体通过阀26送至塔3的顶部冷凝器12，并且将该液体汽化以形成流27，将该流送回至第二塔。将产物流19送至冷凝器20，并且由此处形成流19。流19在热交换器20中冷凝，并且再分为流48(该流在交叉点50处被送至废物流33)以及另一个流。将另一个流通过阀21送至塔4。
纯氩塔4产生产物流45。纯氩塔4的顶部冷凝器13通过阀34进料有源自第一塔的富含氮的液体LP，并且通过阀35以流33的形式取出汽化的氮，并且在再冷却器24中冷却。通过使用空气对纯氩塔的底部再沸器14进行加热，并且将液化的空气23送至第一塔。
同样取出吹扫流46。
通过阀143将富含氮的液体43收集在储存罐144中。
冷凝器20通过阀31进料有富含氮的液体LP，并且将汽化的液体通过阀32送至废物流33。
在热交换器5中朝向该热交换器的冷端冷却并冷凝后，将在65巴下的空气流505再分成两份。在阀231中将部分空气减压并且以液体形式送至塔8和9。
将剩余的空气107再分成三部分107A、107B和107C。在第一级230A与第二级230B之间再循环的空气部分107A对应于总空气流的1.08％。在阀116A中将其从65绝对巴减压至约10.2绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后加热，以提供再循环的空气107A。
在第二级230B与第三级230C之间再循环的空气部分107B对应于总空气流的0.84％。在阀116B中将其从65绝对巴减压至约18.9绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后加热，以提供再循环的空气107B。
在第三级230C与第四级230D之间再循环的空气部分107C对应于总空气流的22.08％。在阀116C中将其从65绝对巴减压至约35.1绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后经加热，以提供再循环的空气107C。
这三个空气部分代表了总的再循环的空气流，其占总空气流的24％，这意味着流体505对应于占总空气流的50.5％的流并且通过阀231的流为26.5％。如可以在图4中看到的，三个空气部分107A、107B和107C的汽化在热交换器5中分别在约-166℃、-155℃和-142℃的温度下发生，这比氧的汽化温度(约-125℃)低。如果经减压的流是两相流体，则必须增加相分离器，液相被引入热交换器5中并且气相与流107混合。术语“冷凝”涵盖蒸汽形式至液体或部分液体形式的冷凝。其还涵盖当超临界流体从高于超临界温度的温度冷却至低于超临界温度的温度时的超临界流体的伪冷凝。
图4呈现了对应于图3的方法的交换图表。
图3的较不优化的替代形式暗示将流107再分为一个或两个部分，并且再循环这些部分，汽化后，使其返回压缩机230。
为了简化以上描述的方法，考虑到107A和107B的低流速，可能的是保留单独的再循环空气部分107C。
可以用液体涡轮机(即产生功的减压系统)代替阀231、116A、116B和116C，目的是为了减少与等焓减压有关的不可逆性。这些液体涡轮机可以并联或串联安装。
在基本的情况下，认为压缩机230是由马达驱动的机器，但是其也可以由蒸汽涡轮机或燃气涡轮机(与用于主空气压缩机6的相同)驱动。作为替代方案，四个压缩机级230A、230B、230C和230D中的任何一个可以由用于减压(优选地在低温下)此空气低温分离方法中的流体的任何一个的机器驱动。此外，四个压缩机级230A、230B、230C和230D中的任何一个可以具有低于环境温度、优选地略高于氧的汽化温度(约-125℃)的吸入温度。就比能量(kWh/Nm3的O2)而言，如果现有技术对应于100，则用于根据本发明在40绝对巴下生产氧所需的比能量为92,9，即节省7.1％。
部分107A、107B和107C可以从通过231的部分空气中分离，并且从热交换器5中在高于热交换器5的冷端的温度的温度下提取。
可以对该方法进行修改，以便汽化泵送的液氮，作为附加的流或作为代替泵送的氧流的流。
同样可能的是在没有被权利要求所涵盖的替代形式中使用氮循环(而不是空气循环)。在此情况下，压缩机230应该进料有至少部分的高压氮气40。
同样可能的是使用本发明减小热交换器5的设计压力，即第二空气压力，凭借流107的再循环而具有较低的能量损耗。
所示出的方法展现了双塔系统，但是易于理解的是本发明适用于三塔系统。
它们还可以与生产低纯度的氧(通常是95％的O2而不是99.5％的O2)的工艺循环，例如“双汽化器”工艺循环一起使用。
在图5的实施例中，提供了使用图3的系统从空气分离单元101开始以更独立的方式从液氧中回收冷量。
特别地，液体容纳罐131、152被添加至储存单元并且释放低温液体，以便使通过ASU生产氧与客户消耗断开连接。此外，它们使得可能减少在高峰时间段的能量消耗，而没有减少流至最终用户的氧流，并且使得可能增加在非高峰时间段的氢的消耗，而没有增加流至最终用户的氧流。
将进料空气在压缩机6中压缩，在纯化单元7中纯化并且再分成两份。
将流505在压缩机230中压缩并且送至热交换器，在其中该流经受部分冷凝、或“伪冷凝”(因其高于临界压力)。在这种情况下，认为压缩机230是离心式压缩机，其包括四级：230A、230B、230C和230D，例如为整体齿轮式，通过水中间冷却器232A、232B、232C以及后冷却器232D冷却。压缩机的吸入压力为5.5绝对巴，中间压力为10.2绝对巴、18.9绝对巴和35.1绝对巴，并且最终压力为65绝对巴。当没有将低温液体储存或从储存中取出时，吸入流为总空气流的23％。
将流505分成第一次级流505A，其直接进入热交换器5，以及第二次级流，其进入制冷单元102以便被冷却至-5℃并引入热交换器5中。
在热交换器5的中间点处，在-124℃的温度下，将第一部分的高压空气取出并送至用于减压的两相装置116D，将其再引入热交换器5中以便加热并在35.1绝对巴下在压缩机230中在级230D作为流107D再循环。此第一部分具有占总空气流的18.4％的流。
将第二部分通过完全通过热交换器5而冷却至-192.2℃并且在阀231中减压，以便将其作为流234送至用于液态空气(LAIR)的储存单元131。此第二部分的流仅为源自主空气压缩机6的总空气流的23％。
将部分107从热交换器5的冷端取出并再分成三份。在第一级230A与第二级230B之间再循环的空气部分107A对应于总空气流的1.1％。在阀116A中将其从65绝对巴减压至约10.2绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后加热，以提供再循环的空气107A。
在第二级230B与第三级230C之间再循环的空气部分107B对应于总空气流的3.15％。在阀116B中将其从65绝对巴减压至约18.9绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后加热，以提供再循环的空气107B。
在阀116C中将空气部分107C从65绝对巴减压至约1.2绝对巴，并且引入热交换器5中，在该热交换器中将其汽化、气化后经加热，以提供再循环的空气107C，如果ASU 101未运行，则该再循环的空气可以用于再生空气净化器。其占总空气流的4.45％。
这三个空气部分107A、107B和107C，以及在涡轮机116D中减压的第一空气部分代表了占源自压缩机230的总空气流的27.1％的总的再循环的空气流，这意味着流体505占源自主压缩机6的总空气流的50.1％，并且通过阀231的流对应于总空气流的23％。
用于通过ASU 101进料的液氧152的储存罐给系统提供氧151。在氧被引入热交换器5之前，液氧泵37将氧加压直至要求的压力水平，氧在该热交换器中经受汽化或伪汽化。
ASU 101进料有源自同一个压缩机6(MAC)的空气510以及液态空气235(用于补偿液氧150的产生)。
在独立于热交换器5的热交换器中通过与源自空气分离单元(未呈现)的氮气热交换将流510冷却。在热交换器5中冷却冷空气是可能的，但是这将使得系统较不灵活。
同样可能的是使空气分离单元和用于回收冷量的此系统处在分开的位置。在这种情况下，应存在给ASU提供空气的压缩机系统以及给冷量回收系统提供空气的另一个压缩机系统，并且可以通过罐或管线进行液态空气235和液氧150的运输。液体储存罐152和131也必须在各自位置处加倍。
当ASU和冷量回收系统在同一位置时，还可能存在给这两个单元提供空气的分开的压缩机系统，如果认为这样更方便和/或更有效率的话。当这两个单元不同时以相同的容量运行时尤其如此。单个压缩机将需要精确的测量程序并且在低容量下将失去其有效性。对于不同的压缩机系统，可以优化每个装置上的测量程序。
为了简化以上描述的方法，考虑到107A和107B的低流速，可能的是保留单独的再循环空气部分107D以及至纯化单元的低压空气107C。
可以用减小液体压力的涡轮机(即产生功的减压系统)代替阀231、116A、116B和116C，目的是为了减少与等焓减压有关的不可逆性。这些减小液体压力的涡轮机可以并联和/或串联安装。
在非高峰时间段期间，当电力的成本比给定值低时，运行空气分离单元，使得储存在储存罐152中的液氧的量增加。在热交换器5中汽化的液氧的量比通过空气分离单元产生的液氧少。
没有空气被送至阀116C，并且通过使用源自空气分离单元101的氮流使纯化单元7再生。
通过独立于热交换器5的热交换器将空气流510送至空气分离单元，并且将空气流235从储存罐131送至空气分离单元，并且将液氧150送至储存罐152。然而，送至容器131的液态空气的量超过从中取出的空气的量，并且送至容器152的液氧的量超过从中取出的液氧的量。
在高峰时间段期间，当电力的成本大于给定值时，不运行空气分离单元、或在低容量(通常是最大容量的50％或更少)下运行，即使总的产生的氧远大于最大容量的50％。没有空气通过流510和235被送至空气分离单元。将储存在罐152中的液氧汽化以提供氧气流。通过使用流107C来进行纯化单元7的再生。
在高峰时间段期间，将通过液氧的汽化产生的液态空气储存在储存罐131中，并且没有气态或液态空气被送至空气分离单元101。
可以对该方法进行修改，以便汽化泵送的液氮，作为附加的流或作为代替泵送的氧流的流。
如图6中所见，同样可能的是使用氮循环(而不是空气循环)。在此情况下，压缩机230进料有至少部分的高压氮气40。然而，在这种情况下，必要的是具有可供使用的氮源，该氮源源自在减小的容量下运行的空气分离单元101、或源自其他空气分离单元，任选地通过氮管道。这是为什么空气是用于此应用的优选的流体的原因，因其独立于任何空气分离单元是可获得的。
在这种情况下，将所有进料空气在主空气压缩机6中压缩直至在ASU101中分离空气所需的压力。
在热交换器5中将经压缩的氮冷却并冷凝。
随后，将经压缩的氮再分成至少两份，在这种情况下是三份，减压至至少两个不同压力，并且在热交换器5中汽化。
将源自阀116A和116B的汽化的氮送回至氮压缩机230的中间位置，并且如果没有运行空气分离单元，则源自阀116C的汽化的氮可用于再生纯化单元。
在阀231中将产生的液氮234减压并且储存在储存单元131中以供使用。
因此，在空气分离单元不运行的时期，例如在电力特别昂贵的时期，液氧可以相对于氮汽化。
在一个或多个空气分离单元的计划的不可用(维护)或计划外的不可用(意外)的情况下，本发明的这些替代形式可以用于从液氧/氮备用系统中回收冷量。
所示出的方法展现了双塔系统，但是易于理解的是本发明适用于三塔系统。其还可以与生产低纯度的氧(通常是95％的O2而不是99.5％的O2)的工艺循环，例如“双汽化器”工艺循环一起使用。

Claims (18)

1.一种用于在塔系统中通过低温蒸馏分离空气的方法，该塔系统包括第一塔和在比该第一塔低的压力下操作的第二塔，该方法包括以下步骤：
i) 在第一压缩机 (6) 中将所有进料空气压缩直至比该第一塔的压力大至多一巴的第一出口压力，
ii) 将在该第一出口压力下的第一部分的空气 (505) 送至第二压缩机 (230)，并且将该空气压缩至第二出口压力，
iii) 在热交换器 (5) 中将在该第二出口压力下的至少部分空气冷却并冷凝，
iv) 将在该第一出口压力下的空气气体流送至该塔系统，没有进行更强力的压缩，并且在该塔系统中分离空气，
v) 从该塔系统的塔中取出液体，将液体加压并且在该热交换器中通过热交换将液体(38) 汽化，以及
vi) 将至少部分的经冷却并冷凝的空气从该第二出口压力减压至至少第三压力，将所述空气在该热交换器中在该至少第三压力下至少部分地汽化，该第三压力为在该第一出口压力与该第二出口压力之间的中间压力，其特征在于，将此空气的至少汽化的部分送至该第二压缩机 (230)，以便将其压缩直至该第二出口压力。
2.如权利要求1所述的方法，其中，该减压在至少一个阀（116A，116B，116C）中进行。
3.如权利要求1所述的方法，其中，该减压在至少一个涡轮机中进行，并且产生功。
4.如权利要求1所述的方法，其中，在减压前的该至少部分的经冷却并冷凝的空气的温度小于该液体的汽化温度和该热交换器中最小温差的总和。
5.如权利要求1所述的方法，其中，该第二压缩机是多级压缩机。
6.如权利要求5所述的方法，其中，所述至少第三压力至少为该第二压缩机的级之一的入口压力。
7.如权利要求5所述的方法，其中，该第二压缩机的级由用于对该方法的流体减压的装置驱动。
8.如权利要求7所述的方法，其中，用于减压的装置的入口温度小于环境温度。
9.如权利要求5所述的方法，其中，该第二压缩机的至少一个级具有小于环境温度的吸入温度。
10.如权利要求9所述的方法，其中，该吸入温度大于该液体的汽化温度，但是与该汽化温度接近。
11.如权利要求1所述的方法，其中，所述第一出口压力基本上等于该第一塔的压力。
12.如权利要求1所述的方法，其中，步骤vi)进一步包括在该热交换器中加热所述至少部分地汽化的空气。
13.如前述权利要求中任一项所述的方法，其中，该液体是富含氧的流。
14.如权利要求1-12中任一项所述的方法，其中，该液体是富含氮的流。
15.如权利要求1-12中任一项所述的方法，其中，一种或多种最终液体产物的生产流不大于进料空气的10%。
16.如权利要求1-12中任一项所述的方法，其中，一种或多种最终液体产物的生产流不大于进料空气的5%。
17.一种用于在塔系统中通过低温蒸馏分离空气的设备，该塔系统包括第一塔和在比该第一塔低的压力下操作的第二塔，该设备附加地包括：
i) 第一压缩机 (6)，其用于将进料空气压缩至比该第一塔的压力大至多一巴的第一出口压力，
ii) 用于将在该第一出口压力下的经纯化并冷却的空气从该第一压缩机送至该塔系统以便在其中进行分离的器件，
iii) 第二压缩机 (230)，以及用于将在该第一出口压力下的第一部分的空气从该第一压缩机送至该第二压缩机的器件，以便将该空气压缩至第二出口压力，
iv) 热交换器 (5)，其中在该第二出口压力下的至少部分空气被冷却并冷凝，
v) 用于从该塔系统的塔中移除液体的器件、用于加压液体的器件 (37)、用于将经加压的液体送至该热交换器的器件、以及用于从该热交换器中移除经汽化的液体的器件，以及
vi) 用于减压在该第二出口压力下的经冷却并冷凝的部分空气的器件、用于将经减压的空气送至该热交换器的器件，
其特征在于其包括用于将在为在该第一出口压力与第二出口压力之间的中间压力的至少第三压力下的已经在该热交换器中被汽化的至少部分所述经减压的空气从该热交换器送至该第二压缩机以便将其压缩至该第二出口压力的器件。
18.如权利要求17所述的设备，其中用于减压的器件是阀或涡轮机。
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FR3062197B3 (fr) 2019-05-10
RU2019140617A3 (zh) 2021-07-19
FR3066809A1 (fr) 2018-11-30
US20200132367A1 (en) 2020-04-30
RU2019140617A (ru) 2021-06-10
US12025372B2 (en) 2024-07-02
CN110678710A (zh) 2020-01-10
FR3062197A3 (fr) 2018-07-27
EP3631327B1 (fr) 2021-06-23
EP3631327A1 (fr) 2020-04-08
WO2018215716A1 (fr) 2018-11-29
FR3066809B1 (fr) 2020-01-31
RU2761562C2 (ru) 2021-12-09

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