CN1918444B - 在空气分离装置中产生加压气态产品的低温空气分离方法 - Google Patents

在空气分离装置中产生加压气态产品的低温空气分离方法 Download PDF

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CN1918444B
CN1918444B CN2004800419880A CN200480041988A CN1918444B CN 1918444 B CN1918444 B CN 1918444B CN 2004800419880 A CN2004800419880 A CN 2004800419880A CN 200480041988 A CN200480041988 A CN 200480041988A CN 1918444 B CN1918444 B CN 1918444B
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air
product
oxygen
liquid
fluid
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CN1918444A (zh
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让-雷诺·布吕热罗勒
B·哈
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • 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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    • 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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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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Abstract

一种在使用蒸馏塔系统(10、11)的空气分离装置中用来产生加压气态产品的低温空气分离过程及设备，其包括：在换热管路(30)内冷却一压缩空气流束以形成压缩的冷却空气流束、输送至少一部分压缩的冷却空气流束至系统的一个塔中、液化(60)工业流束(47)以形成第一液体产品、储存至少一部分第一液体产品到储存罐(50)、将储存罐中的至少一部分上述第一液体产品作为供给(60、61)之一输送至空气分离装置、从塔系统的一个塔中提取至少一第二液体产品流束，并压缩该至少一第二液体产品流束(6)、在换热管路里汽化上述压缩的第二液体产品流束以形成加压气态产品，并提取冷气体(40)(在换热管路里完全没有被加热)。

Description

在空气分离装置中产生加压气态产品的低温空气分离方法
技术领域
本发明涉及一种在空气分离装置中产生加压气态产品的低温空气分离方法。
背景技术
空气分离是一种非常大功率的工艺，其消耗数千千瓦或者数兆瓦的电力来产生大量的例如化学制品、精炼厂、钢厂等吨位使用的工业气体。
图1举例说明了一种典型的液体泵送过程。在这种类型的过程中，大气空气被主空气压缩机(MAC)1压缩到大约6bar的绝对压力，接着在吸附器系统2中净化以除去例如湿气和二氧化碳的杂质而产生净化的进给空气，这些杂质在低温下会冻结。然后，该净化的进给空气的一部分3在换热器30内被冷却至其露点附近，并以气态形式引入双塔系统的高压塔10用于蒸馏。富氮液体4从该高压塔的顶部提取，一部分作为回流被送入低压塔11的顶部。高压塔底部的富氧液体流束5作为供给也被送入低压塔。这些液体4和5在膨胀前被过冷器里的冷气体过冷，为了简化，图中没有示出该过冷器。液态氧6从低压塔11的底部提取、被泵压缩到一期望压力，然后在换热器30中汽化以形成气态氧产品7。为了在换热器30中汽化富氧流束而得到冷凝，该净化的进给空气的另一部分8进一步在升压空气压缩机(BAC)20中被压缩到高压。根据富氧产品的压力，该升压的空气压力可大约为65bar或者有时超过80bar。冷凝的升压空气9也作为供给被送入塔系统用于蒸馏，例如被送入高压塔。液态空气的一部分可从高压塔中提取，并在过冷和膨胀之后送入低压塔。也可能从高压塔的顶部提取富氮液体，然后将其泵送至高压(流束13)，并在换热器中以与液态氧相同的方式汽化。进给空气的一小部分(流束14)被进一步压缩，并在塔11内膨胀以提供装置的制冷。提供制冷的任意备选或者辅助装置都可以使用，例如克劳德膨胀机或者氮膨胀机。
废氮从低压塔顶部提取，并在换热器30内加热。使用标准的其顶部冷凝器由富氧液体5冷却的氩塔可以产生氩。
一个典型的3000吨/天的在压力下产生工业用气态氧的制氧设备会消耗大约50MW。制氧设备的流水线操作网络需要能提供数百兆瓦特电力的电源。事实上，由于其原材料或者供给是大气空气，并且这基本上是自由使用的，所以一个空气分离设备的主要运行成本就是电力。电力用来驱动空气压缩或者产品的压缩机。因此，电力消耗或者过程效率是空气分离装置(ASU)设计和运行中的最重要因素之一。通常表示为$/kWh的电费在一天里不是固定的，但是随峰值或者非峰值相差很大地变化。众所周知，一天内，当需求大时-或者峰值期间-电费最高，而在需求少时-或者非峰值期间-电费最低。如果一个工业电力用户能削减其峰值期间的电力消耗，那么公用事业公司将显著地降低成本。因此，运行空气分离装置的公司总会有强烈的动机去调整设备的运行条件以追踪电力需求量来降低公用事业成本。很清楚，需要为这个可变电费问题提供一个经济的解决方案。
注意到电力峰值出现的时段可能完全不同于产品需求峰值是有帮助的，例如，热的天气将会由于空调设备而需求高电力，而这时，产品的需求保持在正常水平。在一些场所，白天期间，峰值发生在工业气体的主要用户-制造厂的工业输出通常处于最高水平的时候，并且在与其他行为的高电力使用结合时会造成电网的高需求。这种高电力使用引起电势短缺，而公用事业公司必须分配会造成暂时高电费的其他来源的电力供应。此外，一般在晚上，电力需求比较低，并且电力供应比较充足，因此公用事业公司会降低电费以鼓励使用并保持发电设备在减负荷下有效地运行。峰值时的电费可以比非峰值电费高出两倍或者更多倍。在本申请中，术语“峰值”描述的是电费高的时段，而术语“非峰值”意味着电费低的时段。
对于工业电力用户来说，电费通常在供电合同中预先商议并规定。除电费的日常变化外，有时会有一些电力供应中断的预防措施或补贴：在电栅的高电力需求时段，公用事业公司会通过相对短期的提前通知来减少对那些用户的供应，作为回报，所提供的全部电费会明显低于一般的电费。这种调整对用户产生另外的激励以适应其消耗与电力供应者的网络管理相一致。因此，仅当工厂设备可以施行这种灵活性时，可以获得显著的成本降低。基于供电合同中提出的电力成本结构，用户可以规定预定的阈值或者电费阈值以激发减少电力的机制：
-当电费高于预定阈值时，减少电力使用以降低成本。
-当电费低于预定阈值时，增加电力使用到正常水平或者如果要求甚至到更高。
解决变电费问题的一个简单方法是降低设备峰值期间的电力消耗，同时为满足用户需求而保持产品输出。但是，由于其包括蒸馏塔，并且产品规格需要相当高的纯度，所以空气分离设备的低温过程不是非常灵活。试着降低设备很短时间内的输出或者快速增加设备的产生以满足产品需求可能会对设备的稳定性以及产品的完整性产生不利的影响。有许多专利建议如何解决与低温设备的不同产品需求相关的困难。
美国专利3,056,268讲授了储存液体形式的氧和空气的技术，以及汽化这些液体以制造气态产品来满足用户的不同需求，例如在冶金厂。当其需求高时，液态氧被汽化。这种汽化作用被通过双塔空气分离装置的主冷凝器的液态氮的冷凝作用相抵消。
美国专利4,529,425讲授了以类似于美国专利3,056,268的技术解决不同需求的问题，只是使用了液态氮来代替液态空气。
美国专利5,082,482提供了一种美国专利3,056,268的替代形式，其将恒定流量的液态氧送入容器内，并从容器内取出一变流量的液态氧来满足氧的不同需求的要求。取出的液态氧在换热器内通过相应流量的进入空气的冷凝作用而被汽化。
美国专利5,084,081还讲授了美国专利4,529,425的另一种方法，其中，除传统液态氧和液态氮外，另一个中间液体、富氧液体被用作缓冲产品以解决可变的需求。富氧液体的使用使氩塔在可变需求期间稳定。
在另一个解决可变产品需求的方法中，美国专利5,666,823讲授了一种将空气分离装置和高压燃气轮机有效结合的技术。在低产品需求期间，从燃气轮机提取的空气被送入空气分离装置，并且一部分膨胀以生成液体。当产品需求高时，从燃气轮机提取很少的空气，并且早先生成的液体又被送回至系统以满足这种更高的需求。在高产品需求期间，因缺乏从燃气轮机提取的空气而没有运行膨胀机，因此由液体提供的制冷得以补偿。
上述公开内容解决了不同需求的技术问题，尤其是用来在产品需求变化很大的时候保持蒸馏塔稳定性的技术。但是，上述内容没有一个在使空气分离设备适应峰值和非峰值期间电费结构以降低成本时直接解决电势节约和经济的问题。工业实践也没有解决与调整在高电力成本期间的空气分离装置有关的技术问题以及和相对无变化的产品需求有关的技术问题。事实上，空气分离装置运行的这两个问题本质上完全不同：一个受用户的可变需求控制，而另一个受与相对固定的需求有关的可变电费控制。
因此，需要提出一个允许在峰值期间降低电力消耗同时保持产品的供应以满足用户需求的空气分离设备结构。为了弥补这种电力降低，可在非峰值期间以非常低的电费安排其他的电力消耗。由于一部分产品在低电费时产生，而在高电费期间供应给用户，因此可以实现显著的电费节约。
发明内容
本发明提供一种技术，该技术能解决与在峰值期间降低电力消耗同时仍能保持相同产品输出、因此实现电力成本节约有关的问题。
主要方面包括：
a)在非峰值期间液化工业流束以产生第一液体产品；
b)在峰值期间将产生的第一液体产品供给空气分离装置；
c)通过空气压缩机减少空气供给以保持供给流束中含有的全部氧气量基本上相同；
d)从塔系统中提取至少一个产品，并通过泵送作用将其压力升高，接着在换热器内将其汽化以形成气态产品。
e)在低温下从系统中提取冷气体；并且
f)通过冷气体压缩机将该生成的冷气体低温压缩到更高的压力。
具体而言，本发明提供了一种在冷箱内的空气分离装置中产生加压气态产品的低温空气分离方法，其包括下列步骤：
a)在换热管路内冷却一压缩空气流束以形成一压缩冷却的空气流束；
b)将至少一部分被压缩、冷却的空气流束输送至系统的一个塔；
c)仅仅在第一时段内，在电费低于预定阈值时液化工业流束以形成一第一液体产品，并储存至少部分该第一液体产品；
d)仅仅在第二时段内，在电费高于预定阈值时将上述储存的第一液体产品作为供给之一输送至空气分离装置；
e)加压至少一第二液体产品流束；
f)在换热管路内汽化上述加压的第二液体产品流束以形成加压的气态产品；
g)仅仅在上述第二时段内，在电费高于预定阈值时，在-195℃至-20℃之间的温度下从空气分离装置冷箱中提取冷气体；以及
h)相比于当电费低于预定阈值时换热器内的被冷却的空气的量，减少当电费高于预定阈值时换热器内压缩空气的流量。
根据本发明的一个实施例，加压的气态产品是氧产品。
根据本发明的一个实施例，加压的气态产品是氮产品。
根据本发明的一个实施例，步骤c)的工业流束包含任何比例的氧、氮和氩。
根据本发明的一个实施例，步骤c)的工业流束至少是纯氮、空气、至少含37mol％氧的氧中的一个。
根据本发明的一个实施例，步骤g)的冷气体从包括富氮气体、纯氮气、空气、富氧气体以及纯氧产品的组中选择。
根据本发明的一个实施例，步骤e)的第二液体产品与步骤c)的储存的第一液体产品相同。
根据本发明的一个实施例，至少步骤g)的一部分冷气体被加热并在热膨胀机内膨胀以回收能量。
根据本发明的一个实施例，至少步骤g)的一部分冷气体被注入燃气轮机中回收能量。
根据本发明的一个实施例，至少步骤g)的一部分冷气体被循环回流至空气分离装置。
根据本发明的一个实施例，空气分离装置向一IGCC设备供应加压的气态氧产品。
根据本发明的一个实施例，该IGCC设备包括一燃气轮机，该方法进一步包括如下步骤：
i)当电费低于预定阈值时，从燃气轮机中提取空气；以及
j)将上述提取的空气供给到空气分离装置。
根据本发明的一个实施例，该方法包括当电费高于预定阈值时将加压的冷气体注入燃气轮机的步骤。
根据本发明的一个实施例，汽化LNG的制冷被回收以减少第一液体产品的液化成本。
根据本发明的一个实施例，冷气体在没有在换热管路内加热的情形下就从空气分离装置中排除。
根据本发明的一个实施例，冷气体在换热管路内被部分加热之后，从空气分离装置中排除。
根据本发明的一个实施例，冷气体仅在通过横穿换热管路的热端而被冷却之后，从空气分离装置中排除。
根据本发明的一个实施例，步骤c)的工业流束是至少含65mol％氧的氧。
根据本发明的一个实施例，步骤c)的工业流束是至少含85mol％氧的氧。
根据本发明的一个实施例，步骤c)的工业流束是至少含99.5mol％的氧。
附图说明
为了进一步理解本发明的本质和目的，将进行下列和附图有关的详细说明，其中相同的组成部分使用相同或者类似的参考数字。其中：
-图1举例说明现有技术。
-图2举例说明本发明在电费低于预定阈值水平时的情形。
-图2A举例说明本发明在电费高于预定阈值水平时的情形。
-图3举例说明本发明的一个实施方式，以及在非峰值期间液化空气时使用的设备。
-图4举例说明另一个实施方式，其具有一个在非峰值期间液化空气时使用的与空气分离装置连接的独立液化器。
-图5举例说明在空气分离装置中用来产生液态空气的设备。
-图6举例说明峰值期间的液体供给模式。
-图7举例说明冷气体的冷压缩可以单步执行。
-图8举例说明以图2A为基础的空气分离装置，其中冷的低压氮被压缩到绝对值为10至20bar之间。
-图9举例说明经过冷压缩机的冷压缩之后，压缩的冷气体可被加热并输送至热膨胀机用以电力回收或者电力产生。
-图10举例说明本发明的一个应用，其中，压缩的冷气体被输送至燃气轮机用于电力回收。
-图11举例说明一个IGCC应用。
-图12举例说明一种在峰值期间，当液体被供给到系统时，将冷气体从过程中提取的常规方法。
-图13举例说明在电力峰值出现时，空气分离装置的一种运行模式。
具体实施方式
现在，将参照附图更详细地描述本发明。图2-13展示了本发明的空气分离过程。
本发明尤其适合泵送液体的空气分离过程。
该过程至少具有两种运行模式，一个对应于电费低于预定阈值时的时段(图2)，一个对应于电费高于预定阈值时的时段(图2A)。
当电费低于预定阈值时，该设备依照图2如下运行。大气空气被一个主空气压缩机(MAC)1压缩到大约6bar的绝对压力，接着在一个吸附器系统2中净化以除去例如湿气和二氧化碳的杂质而生成净化的供给空气，这些杂质在低温下会冻结。该净化的供给空气的一部分3然后在换热器30内被冷却到其露点附近，并以气态形式引入双塔系统的一个高压塔10用于蒸馏。富氮液体4从该高压塔的顶部提取，并且一部分作为回流被输送至低压塔11的顶部。高压塔底部的富氧液体流束5也作为供给被输送至低压塔。这两个液体4和5在膨胀前过冷。液态氧6从低压塔11底部提取，由泵加压至期望的压力，然后在换热器30内汽化以形成气态氧产品7。净化的供给空气的另一部分8在升压空气压缩机(BAC)20内被进一步压缩至在换热器30内冷凝汽化富氧流束的高压。依据富氧产品的压力，当氧压约为40-50bar或者有时超过80bar时，该升压的空气压力有代表性地约为65-80bar。作为指示，流束8的流量约为压缩机1总流量的30-45％。冷凝的升压空气9也作为供给被输送至塔系统蒸馏，例如被输送至高压塔。液态空气的一部分(流束62)会从高压塔排除，并被输送至低压塔。也可能将富氮液体从高压塔的顶部提取，并接着将其泵输送至高压(流束13)，并在换热器内以与液态氧相同的方式将其汽化。供给空气(流束14)的一小部分被进一步压缩，并在塔11中膨胀以提供装置的制冷。还可以使用能提供制冷的可选方案或者辅助装置，例如克劳德膨胀机或者氮膨胀机。
废氮或者低压氮从低压塔的顶部排除，所有的流束在换热器30内加热。
通过使用标准的、其顶部冷凝器由富氧液体5冷却的氩塔可随意地产生氩。
按照需要，可通过压缩机45、46将氮气压缩到高压以产生氮产品流束48。
在电费低于预定阈值的时段内，空气被图3-5所描述的任何一个装置液化。例如，在图2中，经过吸附器2可获得没有湿气和二氧化碳的气态压缩空气(流束47)，该空气被输送至一个外部液化器60以产生液态空气流束49。该液态空气被储存在罐50内。优选的是，在该阶段，没有液态空气从储存罐50输送至塔。
当电费高于预定阈值时，该设备根据图2A如下所述的运行：
液态空气经与导管9连接的导管60从储存罐50流到高压塔10，并经导管61流至低压塔11。优选的是，在这些阶段，液化器内没有发生空气液化。
当将液态空气从罐50输送至塔系统时，主空气压缩机1的流量可被减少一基本上等同于液态空气量的量，因此可保持该装置供给中氧的总体平衡。如上所述，膨胀机44的流量14很小，可以随意地忽略，所以压缩机1的流量将得到调节。膨胀机的省略会导致制冷功率的损失，这可以容易地通过上述液态空气的数量来补偿。因此，通过流经60的液态空气的流量来代替流束8的流量，压缩机20可以停机，而压缩机1的流量会减少20-55％。这些减少会导致该装置电力消耗的锐减。由于供给塔系统的各种流束的流量近乎相同，所以这些变化不会干扰蒸馏过程，并且产品的纯度也不会受影响。但是，由于供给了大量的液态空气，并省略了升压空气部分9而减少了压缩机1的流量，因此主换热器30在入流和出流以及制冷上都变得不平衡。为了恢复流量以及制冷平衡，应当从系统中提取一个低温的输出冷气体流。图2A举例说明了这种运行的一个可行布置，其中，来自于低压塔的废氮的一部分40在没有在换热器30或者任何一种换热器内加热的情形下从系统中排除。流束40可在其入口处于低温的压缩机70内随意地压缩。冷气体流束可以是任何一种具有适当流量和温度的冷气体，其包括位于低压塔11底部的气态氧产品。离开冷箱的冷气体温度大约在-195℃至-20℃之间，优选的是，位于-180℃至-50℃之间。主换热器30以及其他例如过冷器的低温换热器组成了换热系统、或者有时被称为空气分离装置的换热管路。该换热管路促进了进入的供给气体与流出的气态产品之间的热交换，因此将供给气体在供给塔之前冷却至其露点附近，而将气态产品加热至环境温度。
液化空气所需的电力一般很大，所以通常不会从经济上证实用液态空气代替如上所述的升压空气流束。但是，如前所解释地，由于峰值和非峰值期间的电费差别很大，所以可以想到的是，在电费低，例如晚上的时间段内执行能源密集的空气液化步骤，从而由该液化步骤所产生的成本就不会过大。因此很清楚的是，在峰值期间，可以使用这种早先产生的成本不贵的液体来供给系统以减少该装置消耗的流量或者电力。这种策略极大地减少了装置消耗的电力。因此，支付峰值期间高价电的费用可以减到最小。本质上，这种新发明在低电费期间产生蒸馏所需的气体分子，并有效地在高电费期间使用这些分子以实现总成本的节约。
峰值期间从系统提取的冷气体在低温下被经济地压缩至高压。与环境温度下执行的温压缩相比，这种冷压缩消耗的电力低。事实上，由压缩机齿轮消耗的电力与其入口的绝对温度正好成比例。入口为100K的压缩机齿轮会消耗大约入口为300K的环境温度的压缩机齿轮所消耗电力的1/3。因此，通过使用冷压缩可以在花费相对低的电力需求的条件下增加气体的压缩，进而进一步提高气体的能量值。很明显，从过程提取而不是使其经历冷压缩过程的冷气体可用于其他用途，例如用来冷却别的过程、冷却别的气体等等。根据该申请，通过其他外部回收换热器将冷气体稍微加热至仍是低温(小于-50℃)的另一温度，然后由冷压缩机将其压缩也是可能的，而不是直接冷压缩冷气体。
注意到传统的空气分离装置也经常向环境排放少量的例如冷凝器的不凝清洗或者容器或塔的液体清洗的冷流束是有帮助的。这些清洗流束通常流量很小，一般小于总供给空气的0.2％。除非设置一个可以利用这些清洗流束作为供给的稀有气体(氖、氪、氙等)回收装置，否则就会因其流量太小而没有进行任何冷量回收就将它们排放。同时，该发明回收的冷气体的流量很大：其最小流速大约是供给系统的气态空气最小值的4％，因此差不多是总供给空气速率的70％。
通过使用图3举例说明的不同设备，非峰值期间的空气液化可在另一个低温设备中进行。此时，空气在压缩机100内压缩、被输送至液化器200，然后被输送至储存罐50。峰值期间，该液化空气从储存罐50输送至如图2A所描述的ASU，这种情形下的储存罐位于冷箱外部。
如图4举例说明的那样，通过使用一个与空气分离装置连接的独立液化器也可以实现液化，其中，来自于主空气压缩机1的空气被分成：一部分被输送至液化器200，而剩余部分被输送至ASU。来自于液化器的空气接着又被输送至储存罐50，并在峰值期间由该处返回到ASU。
可选择的是，使用与图5所描述的集成液化器情形下相同的设备，可以在ASU中产生液态空气。图6举例说明峰值期间的液体供给模式。
液体储存罐可以是位于冷箱外部的容器，或者是位于冷箱内部的容器。使用一个底部特别大的蒸馏塔作为液体储存罐也是可能的，此时，储存的液体具有类似于在容器底部生成的液体成分。在填充时，塔或者容器底部的液面可以上升。
现在描述与发明有关的一些附加运行条件的各种过程参数：
-非峰值期间产生的液态空气量取决于非峰值持续时间相对于峰值持续时间的相对长度。非峰值时间越短，所需的液化率越高，反之亦然。在峰值模式下，液态空气的供给率可以约为一般条件下空气总供给率的20-30％。
-图12可用来提供在峰值期间，当液体30被供给系统时，将冷气体从过程中提取的总准则：如图示的那样，塔系统71与换热器65连接，液体产品15、16通过泵20、21被提取到换热器65用于汽化。所有在换热器65内汽化的压缩液体产品的全体被称为总汽化液体。压缩气体31、32在换热器65内被汽化产品15、16冷却和冷凝以生成液体供给25、26，该液体供给接着在塔系统71内膨胀。所有冷凝的压缩流束的总流量被称为总进入液体。冷气体11根据下列准则从系统中提取：其流量约为总汽化液体减去总进入液体的1.6-2.6倍：
冷气体流量＝k[总汽化液体-总进入液体]，其中k＝1.6-2.6
-如上所述，通过增加液态空气的供给量来提取液体产品(氧、氮和连同冷气体一起的那些液体产品的组合)也是可能的，因此产生液体产品或者产品来供应所需的制冷。
附加实施方式
1.冷气体的冷压缩可如上述图2A举例说明的那样单步执行。当压缩冷气体的最后压力比较低时，也就是说，压缩气体的温度保持在低水平时增加压缩气体的流量是可能的，这可以如图7举例说明的那样，通过在换热器30里使来自于冷压缩机70的压缩冷气体冷却来自于主空气压缩机1的辅助空气85(或者氮气)，然后在冷压缩机75内压缩该辅助气体至更高的压力来实现。然后，这两股冷压缩流束在换热器30的上游混合以形成流束95。该换热器可与图2A所示的主换热器30组合。图8也描述了该实施方式。
图8展示了一个以图2A为基础的ASU，其中，冷的低压氮40被压缩至10-20bar的绝对值，优选的是15bar的绝对值。在冷压缩机70内压缩的气体仅在换热器30的热端被加热。在主空气压缩机1中压缩的供给空气的一部分被净化、在换热器30内被冷却至中间温度，然后在冷压缩机75内被压缩至与冷压缩机70出口处相同的压力。在冷压缩机70、75内压缩的这两股流束接着混合，并被输送至例如燃气轮机的燃烧室，在这里，混合流束被加热，接着在叶轮机内膨胀以回收电。
2.图9描述了另一实施方式。在经过冷压缩机70的冷压缩之后，压缩的冷气体被加热，并被输送至热膨胀机110以回收电或者发电。在峰值期间产生的电是非常有价值的，其可以输出以产生附加收入。来自于冷压缩机70的氮在换热器80内加热，并在膨胀机110内膨胀之前进一步由加热器90加热。膨胀机110的废气被输送至换热器80来加热冷的压缩氮。
3.图10举例说明压缩的冷气体被输送至燃气轮机以回收电的应用。此处，来自于冷压缩机70的氮在与来自于燃气轮机压缩机120的空气混合之后，被输送至燃气轮机的燃烧室150。燃料140也被输送至燃烧室，废气通过膨胀机130膨胀以形成气体160。类似于图8或9举例说明的压缩装置也可以在该应用中使用，该压缩装置采用两个压缩机，并将冷压缩空气与冷压缩氮混合。
4.该发明可以用来提高IGCC应用的经济性。事实上，IGCC(集成气化组合循环)过程是以气化煤、石油焦炭等概念为基础的，其使用氧气来产生合成气体(合成气)，该合成气体接着在燃气轮机内燃烧以发电。加入产生蒸汽的子系统以形成辅助的电力产生的组合循环。由于IGCC所需的电通常在白天和晚上变化很大，并且气化器不能随着产生量的变化而变化，所以使用稳定的运行模式是成问题的。另外，该设备在非峰值期间利用不足。还有一个问题是，在环境温度低的晚上，燃气轮机的压缩机会向涡轮机系统产生更多的流量。但是，由于低需求，后一种情况下不会利用这个额外的容量。类似的方式，在白天，当环境温度升高时，燃气轮机的压缩机的流量减少，在这段时间内，需要辅助的电力产生。将这个新发明的特征并入IGCC设备，由于空气分离设备和IGCC的配合，我们可以显著的提高装置的性能：
-晚上，如图11所示，当电需求低并且可以获得更大压缩机流量时，来自于燃气轮机的压缩机120的空气被转移至空气分离设备以提供空气液化所需的至少一部分流量和功率。由于其可以直接使用来自于燃气轮机的提升压力的空气，所以提升压力的ASU也可以方便的使用。由于需要得更多的流量和消耗更多的电力来液化空气，所以在非峰值期间，有更多的合成气用于燃气轮机，IGCC部分可以在夜间保持相对的稳定。图11中，块170代表气化器，块180代表合成气体/燃料处理、过滤、压缩等。
-在白天，由于环境温度的升高，燃气轮机的空气压缩机120的容量减少。夜间模式的空气提取可以停止。然后，夜间产生并被输送至储存罐50的液态空气可用于空气分离设备，该设备的电力消耗减少，因此更多的电力可以转换为白天高需求的供应。此外，ASU提取的冷气体可在冷压缩机70内经济地压缩至更高的压力用于注入燃气轮机，因此平衡了流量的不足，所以产生更多的电。
对于将压缩气体注入燃气轮机或者燃气轮机的应用，图7和8所示的冷压缩装置很适合：注入气体所需的压力大约为15-20bar，该范围正好是那些图的过程所要求的压力范围。通过图示将冷压缩气体流束与冷压缩的富氮气体混合可确保燃烧过程所需氧的良好供应。
本发明可方便地用作蒸馏以及空气分离装置效率的提高。该特点的一个实施方式在图13中举例说明，其描述了电力峰值出现时空气分离装置的一个运行模式。非峰值期间产生的液态空气30被送入塔系统。从蒸馏塔顶部提取的冷气体被冷压缩至和流束13一样的高压。该高压气体的一部分(流束14)循环回流至主换热器65，在此处被液化以形成液体流束15，并被送入塔系统。这种循环回流以及液化作用改善了主换热器65内压缩液体流束23的汽化，因此可以实现液体供给30流量的减少。同样，该液体流束15出现在换热器65的冷端将会平衡设备的冷端部分，并防止流束2的液化。流束2的液化会对换热器65的热交换过程不利，并会引起塔30内的蒸馏问题。如果需要，一部分压缩气体(流束12)也可以被冷却，并在换热管路30内冷却以形成流束16后被循环回流至高压塔的顶部以提高塔系统的蒸馏。在非峰值期间，空气分离设备按照图2所描述的过程运行(为了制图清楚，非峰值模式的膨胀机和压缩机都未示出)。图2的过程是典型的用来泵送液态空气分离设备的过程，对本领域技术人员来说，很显而易见的是，其他液体泵送过程，例如冷的升压过程或者单级克劳德膨胀机液体泵送过程等也可以应用于非峰值模式。峰值期间需要的液态空气可以通过图2所示的外部液化器产生。当然，如前所描述的，也可以使用集成液化器。
附加实施方式也可以应用于从LNG汽化中回收冷量。已经在高峰调节或者汽化末端LNG设备中使用低温设备来回收LNG汽化中释放的冷量。这种制冷被用来降低空气分离设备中产生液体产品的成本。通过本发明，汽化LNG的制冷可被用来降低非峰值期间液态空气的液化成本，因此，如本文所描述的，在峰值期间，当液体被反馈至ASU时，该制冷会节约更多成本。
上述实施方式描述了液态空气被用作中间液体以传递峰值与非峰值期间的制冷和气体分子。对于本领域技术人员来说，显而易见的是，具有空气组成不同成分的任何液体都适用于本发明。例如，液体可以是从高压塔底部提取的含有大约35-42mol％氧的富氧液体、或者是从低压塔底部附近提取的含有70-97mol％氧的液体、或者甚至是纯氧产品。液体也可以是具有少量氧的富氮流束。注意到在峰值期间当该至少不含氧的富氮流束反馈至空气分离装置时，供给的空气流量不再减少，但必须保持恒定以满足氧分子供应是有帮助的。在这样情形下，可以获得电力节约，例如通过使氮产品压缩机(图2的压缩机45、46)停机，并通过明显消耗较少电力的冷压缩机供应氮产品。换句话说，本文适用于具有空气组成任何成分的中间液体。
本发明在变电费结构下的固定产品需求上有发展。很明显，本发明也可以扩展到变产品需求的系统。例如，在氧的低需求期间，可以通过将液态空气供给系统并减少供给空气流量来应用本发明。不用的氧可作为液态氧产品储存，这样蒸馏塔可保持不变。当氧需求大时，该液态氧可以反馈至系统。通过调整液态空气供给、液态氧、冷气体排放以及气态氧供给或者其他类似液态氮的液体的流量，可以提供一个既能满足变产品需求又能满足变电费限制的最佳过程。
虽然本发明参照一定的优选实施方式进行了描述，但是本领域技术人员应当认可在权利要求的实质和范围内的本发明其他实施方式。因此，本发明并不意图被上述所给实例的特定实施方式限制。

Claims (20)

1.一种在冷箱内的空气分离装置中产生加压气态产品的低温空气分离方法，其包括下列步骤：
a)在换热管路内冷却一压缩空气流束以形成一压缩冷却的空气流束；
b)将至少一部分被压缩、冷却的空气流束输送至系统的一个塔；
c)仅仅在第一时段内，在电费低于预定阈值时液化工业流束以形成一第一液体产品，并储存至少部分该第一液体产品；
d)仅仅在第二时段内，在电费高于预定阈值时将上述储存的第一液体产品作为供给之一输送至空气分离装置；
e)加压至少一第二液体产品流束；
f)在换热管路内汽化上述加压的第二液体产品流束以形成加压的气态产品；
g)仅仅在上述第二时段内，在电费高于预定阈值时，在-195℃至-20℃之间的温度下从空气分离装置冷箱中提取冷气体；以及
h)相比于当电费低于预定阈值时换热器内的被冷却的空气的量，减少当电费高于预定阈值时换热器内压缩空气的流量。
2.如权利要求1所述的方法，其特征在于，加压的气态产品是氧产品。
3.如权利要求1所述的方法，其特征在于，加压的气态产品是氮产品。
4.如权利要求1所述的方法，其特征在于，步骤c)的工业流束包含任何比例的氧、氮和氩。
5.如权利要求1所述的方法，其特征在于，步骤c)的工业流束至少是纯氮、空气、至少含37mol％氧的氧中的一个。
6.如权利要求1所述的方法，其特征在于，步骤g)的冷气体从包括富氮气体、纯氮气、富氧气体以及纯氧产品的组中选择。
7.如权利要求1所述的方法，其特征在于，步骤e)的第二液体产品与步骤c)的储存的第一液体产品相同。
8.如权利要求1所述的方法，其特征在于，至少步骤g)的一部分冷气体被加热并在热膨胀机内膨胀以回收能量。
9.如权利要求1所述的方法，其特征在于，至少步骤g)的一部分冷气体被注入燃气轮机中回收能量。
10.如权利要求1所述的方法，其特征在于，至少步骤g)的一部分冷气体被循环回流至空气分离装置。
11.如权利要求1所述的方法，其特征在于，空气分离装置向一IGCC设备供应加压的气态氧产品。
12.如权利要求11所述的方法，其特征在于，该IGCC设备包括一燃气轮机，该方法进一步包括如下步骤：
i)当电费低于预定阈值时，从燃气轮机中提取空气；以及
j)将上述提取的空气供给到空气分离装置。
13.如权利要求11所述的方法，其特征在于，包括当电费高于预定阈值时将加压的冷气体注入燃气轮机的步骤。
14.如权利要求1所述的方法，其特征在于，汽化LNG的制冷被回收以减少第一液体产品的液化成本。
15.如权利要求1所述的方法，其特征在于，冷气体在没有在换热管路内加热的情形下就从空气分离装置中排除。
16.如权利要求1所述的方法，其特征在于，冷气体在换热管路内被部分加热之后，从空气分离装置中排除。
17.如权利要求16所述的方法，其特征在于，冷气体仅在通过横穿换热管路的热端而被冷却之后，从空气分离装置中排除。
18.如权利要求5所述的方法，其特征在于，步骤c)的工业流束是至少含65mol％氧的氧。
19.如权利要求18所述的方法，其特征在于，步骤c)的工业流束是至少含85mol％氧的氧。
20.如权利要求19所述的方法，其特征在于，步骤c)的工业流束是至少含99.5mol％的氧。
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