CN105473968A - 用于以可变的能量消耗通过空气的低温分离产生氧的方法和装置 - Google Patents

用于以可变的能量消耗通过空气的低温分离产生氧的方法和装置 Download PDF

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CN105473968A
CN105473968A CN201480039430.2A CN201480039430A CN105473968A CN 105473968 A CN105473968 A CN 105473968A CN 201480039430 A CN201480039430 A CN 201480039430A CN 105473968 A CN105473968 A CN 105473968A
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condenser
air
nitrogen
stream
pressure column
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CN105473968B (zh
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L·基希纳
D·戈卢贝夫
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Linde GmbH
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Linde GmbH
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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
    • F25J3/04006—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
    • F25J3/04054—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 of 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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    • 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
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    • F25J3/0406—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 of nitrogen
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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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    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
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    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
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    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
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    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of nitrogen
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    • 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
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/62—Purifying more than one feed stream in multiple adsorption vessels, e.g. for two feed streams at different pressures
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    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
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    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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Abstract

本方法和装置用于以可变的能量消耗通过空气的低温分离产生氧。蒸馏塔系统包括高压塔(34)、低压塔(35)和主冷凝器(36)、副冷凝器(26)和附加冷凝器(37)。来自所述高压塔(34)的气氮(41、42)在所述主冷凝器(36)中被液化，与来自低压塔(35)的中间液体(43)间接热交换。来自所述低压塔(35)底部的第一液氧流(70)在所述副冷凝器(26)中蒸发，与供给空气(25b)间接热交换以获得气氧产品(72)。所述附加冷凝器用作低压塔(35)的底部加热装置，并借助来自所述蒸馏塔系统的第一氮流(44)进行加热，其中氮流预先在所述冷压缩机(45)中被压缩。在能量消耗更低的第二运行模式中，更少的供给空气(1)在设备的主空气压缩机(3)中被压缩至比能量消耗更高的第一运行模式中更低的压力，来自所述低压塔(35)的更少的液氧(70)流入所述副冷凝器(26)中，且更多的氮在所述冷压缩机(45)中被压缩。而且，在第二运行模式中，第二液氧流(73)另外流入副冷凝器(26)中。

Description

用于以可变的能量消耗通过空气的低温分离产生氧的方法和装置
本发明涉及一种根据专利权利要求1之前序部分所述的方法。本发明的方法和装置特别适于产生气态的不纯的氧。在此“不纯的氧”被理解为具有少于98％mol纯度的产品。
用于空气的低温分离的方法和装置是已知的，例如，出自豪森/林德(Hausen/Linde)，Tieftemperaturtechnik，第二版，1985，第4章(第281-337页)。
蒸馏塔系统可以是双塔系统的形式(例如传统的林德(Linde)双塔系统的形式)或可选地为具有三个或更多个塔的形式。除用于氮氧分离的塔之外，它还可以具有用于产生高纯产品和/或其它空气成分(特别是稀有气体，例如氩产品和/或氪-氙产品)的装置。
本文的“低压塔”被理解为均匀的蒸馏区域，其中除在物质交换元件中的自然压力损失之外，压力为恒量。该蒸馏区域可以布置在一个或多个容器中。
“主热交换器”用于冷却与来自蒸馏塔系统的返回流间接热交换的供给空气。它可以是单个热交换器部分或并联和/或串联的多个热交换器部分的形式，例如一个或多个板式热交换器单元。
“冷凝器-蒸发器”涉及一种热交换器，其中第一冷凝流体流与第二蒸发流体流发生间接热交换。每个冷凝器-蒸发器具有液化空间和蒸发空间，其分别由液化通道和蒸发通道组成。在液化空间中实施第一流体流的冷凝(液化)；在蒸发空间中实施第二流体流的蒸发。所述蒸发和液化空间由多组通道形成，这些通道彼此之间是热交换关系。
“侧冷凝器”被理解为冷凝器-蒸发器，其设计成几乎专门用于将来自冷凝过程流蒸发的潜热间接传递至与第二冷凝过程流相对的蒸发过程流，且其不适于或基本不适于显热的传递。所述“侧冷凝器”由独立于其他热交换器的热交换器形成，特别是主热交换器或过冷却逆流热交换器，二者通常单独地或主要地用于纯的气态流的热交换。
本文中流的“量”是指物质流率，例如以Nm3/h为单位。
在本申请中，过程参数例如质量流或压力多次被描述为，其在一个运行模式中比在另一个运行模式中“更小”或“更大”。这意味着通过调整和/或控制装置有目的地改变相应参数，而不是在稳态运行状态内的自然变化。这些有目的的改变可通过调节参数自身直接地作用，或通过调节影响被改变参数的其他参数间接地作用。特别地，当不同运行模式中的参数平均值之间的差大于2％，特别是大于5％，特别是大于10％时，参数为“更大”或“更小”。
“第一液氧流”是从低压塔排出并引入到侧冷凝器的蒸发空间中的液氧的质量流。它可以是从低压塔排出的液氧的总量。然而，例如当液氧产品额外地从低压塔获得并供给至液罐，第一液氧流也可以由从低压塔排出的仅一部分液氧组成。如果从侧冷凝器的蒸发空间提取液氧产品，则它通常由“第一液氧流”的一部分形成。反之，除第一液氧流之外，大体上可将液氧供给至侧冷凝器。
“第二液氧流”表示引入到侧冷凝器的蒸发空间中的液氧的总量与第一液氧流之间的差。例如第二液氧流从液罐排出。液罐可单独地由外部源充装，单独地由来自低压塔(如在施普林曼(Springmann)中，参见下文)的液氧充装，或部分由外部液氧充装而部分由蒸馏塔系统特别是低压塔或侧冷凝器的蒸发空间中形成的液氧充装。
开头所述的方法类型和相应的装置是已知的，出自施普林曼(Springmann)，“Energieeinsparung”，林德-论文集“Luftzerlegungsanlagen”，1980年10月15日至17日的林德股份公司的第四次研讨会，文章H。其中示出了具有两个液罐的可选择的储存方法。然而，凭借具有可变产量的蒸馏塔系统实施该方法不具有恒定的生产能力，而是依赖于可变的能量消耗而具有可变的运行。当能源价格低时，产生氧作为库存，并存储在液罐中。当能源价格高时，将空气的量减少，且将一部分氧产品从库存中排出。因此，作用在库存氧上的分离功可用于能量储存。根据该教导，在便宜能量时期，在工厂中液体空气由液氧替代，那就是说将液氧供给到罐中，而将等量的液体空气从相应的罐供给到蒸馏塔系统中。反之，在高电价时期，将来自罐的液氧供给到系统中，并储存液体空气。因此，几乎仅仅储存的氧分子被用于能量储存；在高电价时期，主空气压缩机必须传送相应的更少的分离空气。
本发明的根本目的在于在能量储存方面提高此类方法的效率。
该目的通过专利权利要求1所描述的特征来实现。
与传统的林德双塔不同，虽然其也用于施普林曼，但是主冷凝器不是配置为低压塔的底部蒸发器，而是中间蒸发器。它可布置在低压塔内或分离容器中。低压塔的底部通过附加冷凝器加热，所述附加冷凝器通过冷压缩的氮流加热。来自低压塔下部区域的氧流，其在附加冷凝器中蒸发，优选地来自材料交换元件(填料或塔板)的最下层，在这种情况下，附加冷凝器建在低压塔的容器内；可选地，它可从低压塔的底部抽取，特别是当附加冷凝器被布置在分离容器中时。在两种情况下，侧冷凝器的第一液氧流优选地从附加冷凝器的蒸发空间(在附加冷凝器建在塔内的情况下，其同时构成低压塔的底部)排出。所有的冷凝器-蒸发器因而可以是水浴蒸发器、降膜蒸发器或者也可以是不同类型的冷凝器-蒸发器的形式。
此类冷凝器配置本身从US6626008B1或US2008115531A1中可知，但仅用于在稳态条件下内部压缩过程中运行的方法，液氧流的蒸发发生在主热交换器中，供给空气也在其中冷却，而不是在分离的侧冷凝器中。尽管US2008115531A1涉及具有可变能量消耗的运行，但使用这种方法仅能实现小范围的变化。
首先，本领域技术人员会避免使在冷压缩机中压缩的第一数量的氮发生变化，因为这意味着附加冷凝器的可变运行以及由此在低压塔中蒸馏的可变运行，其原则上使得分离过程效率降低，在不利的环境下，会与塔中的材料交换发生非常大的干涉。
仅在本发明的范围内，发明人发现，通过改变在冷压缩机中压缩并用于加热低压塔底部的氮量，可以不仅有效地利用包含在将要供给的液氧中的分离功，还有效地利用包含其中的冷量(也为了部分地补偿在液化方面与其相关的花费)。这可以作如下解释：在第二运行模式中，附加冷凝器的蒸发能力增加，而主冷凝器的蒸发能力相应地减少。增加附加冷凝器的蒸发能力会增加气体负荷，并减少在低压塔的最后(下层)部分的回流比。这所产生的结果是将在主冷凝器中蒸发的液体中的氧含量降低，并且高压塔(其原则上相当于主空气压缩机的输出压力减去压力损失)中的压力相应地减少。由于在主空气压缩机中的较低的压比-除在量上的减少之外-每一储存的液氧量(LOX)所具有的特别大量的能量可以在第二运行模式中节省下来。
另一方面，在US2008115531A1中，主冷凝器的回流比和蒸发能力都不会受到影响。尽管侧冷凝器的蒸发能力发生变化，但这仅用于可从外部供给的液氧的蒸发，相应地既不能减少主冷凝器的蒸发能力，也不能减少高压塔的运行压力，因而不能减少主空气压缩机的输出压力。
在本发明的内容中，如果不通过一个或多个诸如节流阀的控制元件人为地减少主空气压缩机的出口与进入高压塔的入口之间的压力，则未必需要用于减少主空气压缩机输出压力的特殊规则或调节措施。
在本发明其它实施方案的内容中，第一氮流在冷压缩机的下游和主热交换器中的附加冷凝器的液化空间的上游被冷却。冷压缩机的压缩热因而不在附加蒸发器中减少，而在主热交换器中减少。因此附加蒸发器特别有效地工作，特别是在第二运行模式下。总之，在第二运行模式下能够节省甚至更多的能量。
此外，在第二运行模式下膨胀机可以被关闭或停止，如专利权利要求3中所述。
对比根据施普林曼的方法，在本发明中，在第二运行模式下优选地没有液态空气产生并储存在液罐中。此外，有利的是，在第二运行模式下没有产生来自蒸馏塔系统的馏分作为液氮并储存在液罐中，像在其它传统的可选的储存器过程中。
根据本发明的其他的实施方案，将在主空气压缩机中压缩的空气在将其引导进入主热交换器中的上游处分流为第一和第二部分空气流，其中第二部分空气流进一步地在增压空气压缩机中压缩，且将进一步压缩的第二部分空气流引入到侧冷凝器的液化空间，并在其中至少部分地液化。总的空气因而仅需要在主空气压缩机中压缩至高压塔的运行压力加上管路损失的压力。
通过使用增压空气压缩机，能够在显著高于低压塔运行压力的压力下获得气氧产品。然而，增压空气压缩机在本发明中具有其它有利的作用，其体现在即使在不显著高于低压塔压力的压力下也能获得氧产品。也就是说，它减少了运行附加冷凝器所需的冷压缩机的电力。
供给空气的分流可在用于空气的提纯装置的上游或下游实施。在第一种情况下，特别需要具有用于两个压缩级的二级单位的提纯装置。在WO2013053425A2中描述了特别有利于在根据本发明的方法中使用的空气提纯的系统，其属于相同的申请人。
在本发明中，第二氮流能够以气体形式从高压塔中排出，在主热交换器中加热，并以增压的气氮产品的形式排出。因而能够获得增压的氮，作为相对低价的附加气体产品。
可选地或此外，以气体形式从高压塔排出第三氮流，在主热交换器中将它加热至中间温度，然后使它优选地在上文所述的可变运行的膨胀涡轮中膨胀以执行工作，由此在第一运行模式或两种运行模式中都可以使用来自高压塔的氮以产生冷。作为替代，也可以在空气喷射涡轮中产生冷量，在其中将供给空气的一部分膨胀至低压塔压力以执行工作，并直接供给进入低压塔中。
低压塔和高压塔大体上可彼此邻近地布置。如果低压塔和高压塔一个布置在另一个之上，在本发明中就能够获得特别的紧凑布置，即形成传统的双塔。通过将低压塔和两个冷凝器布置在一个普通容器中，主压缩机和附加冷凝器优选地建在双塔内。
具体而言，当塔一个布置在另一个之上时，如果在低压塔的头部供给的回流液体的至少一部分、特别是全部是由附加冷凝器中产生的一部分液氮形成的，则是有利的。这具有比主冷凝器中形成的氮更高的压力，并因此不需要泵就能够流向低压塔的头部。尽管塔一个在另一个之上布置，则优选仅需要单独的低温过程泵，即用于将高压塔底部液体输送至低压塔中适当的供给点。(可用于提高侧冷凝器上游的液氧压力的泵不包括在“过程泵”中。)
本发明还涉及根据专利权利要求11的一种用于通过具有可变能量消耗的空气低温分离产生氧产品的装置。根据本发明的装置可通过与从属方法权利要求特征相应的装置特征得到补充。
“用于在第一和第二运行模式之间切换的设备”是复杂的调整和控制装置，且当一起使用时，该装置例如通过相应的编程的可操作的控制系统，允许在两个运行模式之间至少部分地自动切换。
本发明和本发明的其它细节将通过附图中示意性示出的实施方案更详细地描述，其中：
图1示出了本发明具有增压的氮产品的第一实施例；
图2示出了第一实施方案的变形，其中增压的氮在热涡轮(热气体膨胀机)中至少间歇地膨胀以执行工作；
图3示出了另一个具有热耦合的实施方案；和
图4示出了第四实施方案，其具有并排布置的塔并且将主热交换器的一组通道切换。
下面首先参照第一运行模式(此处：在能源价格相对低时的正常运行)描述图1的方法。大气空气1(AIR)经过滤器2从主空气压缩机(MAC)3引出，并压缩至例如3.6bar的压力。在主空气压缩机中压缩的总空气流4在第一直接接触冷却器5中通过与水直接逆流的方式预冷却。在第一直接接触冷却器5的下游，将总空气流6分流为第一部分空气流10和第二部分空气流20。
第一部分空气流10在第一纯化单元11中纯化，并以主空气压缩机的出口压力减去管路损失的压力，经管路12供给至主热交换器的热端。在该实施例中主热交换器由两部分32、33形成，其在空气侧并联连接，并优选地都由板式热交换器块形成。经纯化的第一部分流12的最大部分13被供给至第一部分32，在其中冷却至大约露点，并经管路14流至蒸馏塔系统的高压塔34。该蒸馏塔系统另外还具有低压塔35以及三个冷凝器-蒸发器，即主冷凝器36、附加冷凝器37和侧冷凝器26。所述主冷凝器和附加冷凝器是降膜蒸发器的形式，而侧冷凝器是水浴蒸发器的形式。在该实施例中，高压塔34的运行压力大约为3.27bar，低压塔35的运行压力大约为1.28bar(在每种情况下的头部位置)。
第二部分空气流20包括大约四分之一的总空气量6，并在增压空气压缩机(BAC)21中进一步压缩至例如5.1bar。所述进一步压缩的第二部分空气流22在第二直接接触的冷却器23中通过与水直接逆流来用水进行预冷却。在第二直接接触冷却器23的下游，预冷却的第二部分空气流在第二净化单元24中被纯化。在增压空气压缩机21的出口压力减去管路损失的压力下，经纯化的第二部分空气流25a被供给至主热交换器32的热端，在其中冷却。经冷却的第二部分流25b在侧冷凝器26中至少部分优选地全部或基本上全部液化，且第一部分经节流阀28在高压塔34的中间点被引入。第二部分29流经过冷却逆流热交换器30，并经节流阀31在低压塔35的中间点供给。
富氧底部馏分38从高压塔34的下层区域以液体形式排出，并借助泵39供给通过过冷却逆流热交换器30，并经节流阀40进入低压塔35。
气氮经管路41在高压塔34的头部被引出。其中的第一部分42供给进入主冷凝器36的液化空间，在其中相对于来自低压塔35的蒸发的中间馏分43至少部分地液化。由此产生的液氮43供给返回高压塔34的头部，在其中用作回流。
将来自高压塔34头部的气氮41的第二部分作为“第一氮流”44在冷压缩机45中压缩至大约4.8bar。冷压缩的第一氮流46在主热交换器32中再次被冷却至大约露点，并经管路47供给至附加冷凝器37的液化空间，在其中它与低压塔35的部分蒸发的底部液体66间接热交换而至少部分地液化。由此产生的液氮48的第一部分49通过过冷却逆流热交换器30，并作为回流经节流阀50进入低压塔35的头部；其第二部分51作为回流进入高压塔34。
来自高压塔34头部的气氮41的第三部分经管路53流入主热交换器32的冷端。其一部分被加热至环境温度，并作为“第二氮流”经管路54被引出，并作为增压的气氮产品(PGAN)被排出。另一部分55同样被完全加热，并出于辅助目的而在工厂内使用，例如作为压缩气体。(在本发明的所有实施方案中，此类增压的氮产品和/或氮辅助气体的产生是可能的，但不是必需的。同样也适用于图2和3的系统。)
来自高压塔34头部的气氮41的另一部分56在主热交换器32中作为“第三氮流”以中间温度分流出来，并在膨胀机57中膨胀至恰好高于环境压力，所述膨胀机57为冷发生器涡轮的形式。膨胀以执行工作的第三氮流58在主热交换器32中被加热至大约环境温度。如果热的第三氮流59不经管路60和61排出直接进入大气(ATM)，则它可选地在再生气体加热器64、65之一(由冷凝蒸汽(STEAM)运行的)中加热后，作为再生气体62、63用在纯化装置11、24中。
来自低压塔头部的剩余气体67在过冷却逆流热交换器30中以及在主热交换器32中被加热，并最终作为干气体经管路68供给进入用于冷却冷却水的蒸发冷却器中。
作为“第一液氧流”的液氧在大约1.5bar的压力下经管路70供给进入侧冷凝器26的蒸发空间，在其中它几乎完全蒸发。经蒸发的氧71在主热交换器32中被加热，并经管路72作为气氧产品(GOX)被获得。来自侧冷凝器26的蒸发空间的冲洗液体75在泵76中达到超临界压力，并在主热交换器的部分33中相对于空气流14伪蒸发和加热。随后，经加热的流节流并与热的气氧产品混合，由此只提供单一的氧产品。
在第一运行模式下，没有从液氧罐74通过管路73进入侧冷凝器26的蒸发空间的流量。
另一方面，在第二运行模式下，将来自液体罐74的液氧作为“第二液氧流”经管路73被引入侧冷凝器。此外，与第一运行模式相比，下列过程参数发生改变，具体如下：
-冷压缩机45的能力从70％增加至100％。(从而在冷压缩机中压缩的氮的量增加仅大约8％。因为冷压缩机的吸入压力根据高压塔的运行压力而减少，其在能力上出现显著的较大增加。)
-主空气压缩机的能力降至大约80％。
-在主空气压缩机3的出口处的总空气压力减少大约14％，例如从大约3.65bar减至大约3.15bar。
-增压空气压缩机21的能力从大约80％增加至100％。
-冷压缩机45的能力从大约70％增加至100％。
-通过膨胀涡轮57的氮的量从100％减少至0％(也就是说，膨胀涡轮在第二运行模式下不运转)。
如果在不同实施方案中多个(例如两个)并联的冷压缩机用在相同的位置，则有可能达到甚至更高的效率。在第二运行模式中开启第二冷压缩机，这样随后能够达到两倍的能力。在这种情况下，主空气压缩机能够在最小负荷下运行，而更小的增压空气压缩机能够在它的最大负荷下运行。因为大约90％的总能量消耗需要用于驱动主空气压缩机，所以过程变得更有效，主空气压缩机的更多能力可减少，即使冷压缩机的能力从而增加。
(与在此所示的实施方案不同，工厂可设计成用于最大量的氧产品，其高于第一或第二运行模式的氧产品量，也就是说在第一和/或第二运行模式中获得比设计情况更小量的气氧产品72。在此本发明的方法是灵活的，只要不超出所使用的机械的运行范围。)
如果冷压缩机在第一运行模式下以尽可能低的能力运行，而主空气压缩机设计为在第一运行模式下以它的额定能力的大约100％运行，则在本发明中通常是有利的。另一方面，增压空气压缩机和氮冷压缩机设计为例如具有在第二运行情况下所需的能力。
借助这些措施，在第二运行模式下过程中消耗的总能量被减少至在第一运行模式下的数值的大约86％，尽管气氮72的产量相等或仅稍微低。如果液氧的供给是充足的，则能够获得用于能量储存的相应利润。
图2与图1的不同在于没有增压的气氮产品产生。作为替代，在第二运行模式下，直接从高压塔获得的氮产品254在加热器255中达到显著高于环境的温度，并在热膨胀涡轮(热气体膨胀机)256中膨胀以执行工作。因此，利用耦合到加热器255中的剩余热量，在高能量价格时期在连接至膨胀涡轮256的发生器中能够获得特别有价值的电能。如果在其它方面不能经济利用的废热(例如来自低压蒸汽)被用于加热器255，则在这种情况下在第二运行模式与第一运行模式相比，能够达到空气分离过程所需的能量中大约76％的总减少量。
在与图2相关的变形实施方案中，至少在第一运行模式下，可选择也在第二运行模式下，直接从高压塔排出的氮的一部分在第一运行模式中被用于生成增压的气氮产品(参见图1中的PGAN)。
图3的方法与图1的方法的不同在于压缩机冷却与例如属于电厂的蒸汽循环之间的热耦合。经位于两个直接接触冷却器上游的附加冷却器301和302，将来自空气压缩的压缩热量输送到用于电厂工艺的供给水(供给水至电厂)。
此外，图3还示出了如何将在侧冷凝器中未蒸发的第一液氧流的一部分在第一运行模式下经管路303部分地引出，可选地在过冷却逆流热交换器30中冷却，并作为液氧产品(LOX)排出。该液氧产品可全部或部分地引入液罐74中。同样在本发明的所有其它实施方案中(例如根据图1或2的示例)，在第一运行模式下以这种方式能够获得液氧，随后该液氧形成在第二运行模式下经管路73供给的液氧的一部分或全部。
在图4的系统中，高压塔34和低压塔35并排布置。此外，附加冷凝器37(低压塔35的底部加热)位于高压塔34的上方。在该具体的实施例中，侧冷凝器26位于高压塔34和附加冷凝器37之间。
此外，图4还示出了压缩机冷却和蒸汽循环之间的热耦合的一部分，其已经在图3中示出，即冷却器301，其通过来自电厂工艺的供给水而运行。
在图4中，该热耦合与热膨胀涡轮(热气体膨胀机)256相结合，其在图2中详细地进行了解释。此外还提供有具有安全阀的管路401。
对比图2，在用于图3方法中的流447、453、454的主热交换器32a、32b中无需单独的热交换器通道。而不是在交替的运行中，所述流通过与涡轮膨胀流58相同组的通道。为了那个目的，阀402在第一运行模式中，而阀403关闭。反过来，在第二运行模式下，涡轮57静止，阀402关闭而阀403打开。这导致了主热交换器32a、32b的特别紧凑的结构。
图4的所有其它特征在图1和3中描述。

Claims (11)

1.一种用于在蒸馏塔系统中以可变的能量消耗通过低温分离空气来产生氧的方法，该蒸馏塔系统具有高压塔(34)、低压塔(35)以及均为冷凝器-蒸发器形式的主冷凝器(36)和侧冷凝器(26)，其中在所述方法中
-将大气空气(1)在主空气压缩机(3)中压缩至总空气压力，在主热交换器(32、33)中冷却，并至少部分供给至所述高压塔(34)，
-在所述主冷凝器(36)中，来自所述高压塔(34)的气氮(41、42)被至少部分液化，
-在所述主冷凝器中产生的液氮(43)的至少一部分作为回流被用在所述蒸馏塔系统的至少一个塔中，
-将来自所述低压塔底部的第一液氧流引入所述侧冷凝器(26)中，并在其中与经压缩并冷却的供给空气的至少一部分(25b)间接热交换而至少部分地蒸发，
-所述经蒸发的第一液氧流(71)的至少一部分作为气氧产品(72)被获得，
在具有更高能量消耗的第一运行模式中
-将来自所述低压塔(35)底部的第一数量的第一液氧流(70)引入所述侧冷凝器(26)中，和
-在所述主空气压缩机(3)中将第一数量的空气压缩至第一出口压力，
在第二运行模式Au中
-在所述主空气压缩机(3)中压缩第二数量的空气，所述第二数量的空气比第一数量的空气少，
-将来自所述低压塔(35)底部的第二数量的第一液氧流(70)引入所述侧冷凝器(26)中，所述第二数量比第一数量少，和
-除所述第一液氧流(70)之外，将第二液氧流(73)供给至所述侧冷凝器(26)，
其特征在于：
-在两种运行模式中
-将来自所述低压塔(35)中间点的中间液体(43)引入所述主冷凝器(36)的蒸发空间中，并将至少一部分在所述主冷凝器中产生的蒸汽引入所述低压塔(35)中，
-将氧流(66)从所述低压塔(35)的下层区域排出，并通入冷凝器-蒸发器形式的附加冷凝器(37)的蒸发空间中，
-将至少一部分在所述附加冷凝器的蒸发空间中形成的气体作为上升蒸汽引入所述低压塔(35)中，
-将所述侧冷凝器(26)中蒸发的氧(71)在所述主热交换器(32)中加热，并作为气氧产品(72)获得，
-将来自所述蒸馏塔系统的第一氮流(44)在冷压缩机(45)中压缩，然后至少部分被引入所述附加冷凝器(37)的液化空间，和
-将至少一部分在所述附加冷凝器(37)中生成的液氮作为回流用在所述蒸馏塔系统的至少一个塔(34、35)中，其中
在第一运行模式中
-在所述冷压缩机(45)中压缩第一数量的氮，
-将来自所述高压塔(34)中的第一数量的气氮(41、42)引入所述主冷凝器(36)中；和
-在所述主空气压缩机(3)中将第一数量的空气压缩至第一总空气压力，以及
在第二运行模式中
-在所述冷压缩机(45)中压缩第二数量的氮，所述第二数量的氮多于第一数量的氮；
-将来自所述高压塔(34)的第二数量的气氮(41、42)引入所述主冷凝器(36)中，所述第二数量少于第一数量，和
-在所述主空气压缩机(3)中将第二数量的空气压缩至低于第一总空气压力的第二总空气压力。
2.如权利要求1所述的方法，其特征在于，在位于所述冷压缩机(45)下游和所述附加冷凝器(37)上游的主热交换器(32)中冷却所述第一氮流(44)。
3.如权利要求1或2所述的方法，其特征在于，
-在第一运行模式中，第一涡轮流量(56)在膨胀机(57)中膨胀以执行工作，然后在所述主热交换器(32)中被加热和/或引入所述蒸馏塔系统中，和
-在第二运行模式中，所述膨胀机(57)不运行或将第二涡轮流量引入所述膨胀机中，所述第二涡轮流量少于第一涡轮流量。
4.如权利要求1-3中任一项所述的方法，其特征在于，在所述第二运行模式中，没有液态空气产生并储存在液罐中。
5.如权利要求1-4中任一项所述的方法，其特征在于，在所述第二运行模式中，没有馏分作为液氮从所述蒸馏塔系统排出并储存在液罐中。
6.如权利要求1-5中任一项所述的方法，其特征在于，在所述主空气压缩机(3)中压缩的空气(4、6)在它引入主热交换器(32、33)中的上游被分流为第一和第二部分空气流(10、20)，其中所述第二部分空气流(20)在增压空气压缩机(21)中进一步压缩，并将所述进一步经压缩的第二部分空气流(22、25a、25b)至少部分引入所述侧冷凝器(26)的液化空间中，并在其中至少部分液化。
7.如权利要求1-6中任一项所述的方法，其特征在于，第二氮流(53)以气体形式从所述高压塔(34)排出，在所述主热交换器(32)中被加热，并作为增压的气氮产品(54)排出。
8.如权利要求1-7中任一项所述的方法，其特征在于，第三氮流(254)以气体形式从所述高压塔(34)排出，在所述主热交换器(32)中加热至中间温度，并随后膨胀(256)以执行工作。
9.如权利要求1-8中任一项所述的方法，其特征在于，所述低压塔(35)和所述高压塔(34)一个在另一个之上地布置。
10.如权利要求1-9中任一项所述的方法，其特征在于，至少一部分、特别是全部的在低压塔(35)的头部供给的回流液体由所述附加冷凝器(37)中产生的液氮(48)的一部分(49)形成。
11.一种用于以可变的能量消耗通过低温分离空气以产生氧的装置，其具有
-蒸馏塔系统，其具有高压塔(34)、低压塔(35)以及均是冷凝器-蒸发器形式的主冷凝器(36)和侧冷凝器(26)，
-具有用于压缩大气空气(1)的主空气压缩机(3)，
-具有用于冷却压缩空气的主热交换器(32、33)，
-具有用于将所述冷却空气引入所述高压塔(34)中的设备，
-具有用于将气氮(41、42)从所述高压塔(34)引入所述主冷凝器(36)的液化空间中的设备，
-具有用于将所述主冷凝器中生产的液氮(43)作为回流引入所述蒸馏塔系统的至少一个塔中的设备，
-具有用于将第一液氧流(70)从所述低压塔(35)的底部引入所述侧冷凝器(26)的蒸发空间中的设备，
-具有用于将经压缩并冷却的供给空气引入所述侧冷凝器(26)的液化空间中的设备，
-具有用于获得至少一部分所述蒸发的第一液氧流(71)作为气氧产品(72)的设备，
-和具有用于在第一和第二运行模式之间切换的设备，其中
在具有更高能量消耗的第一运行模式中
-将来自所述低压塔(35)底部的第一数量的第一液氧流(70)引入所述侧冷凝器(26)中，和
-在所述主空气压缩机(3)中压缩第一数量的空气，
在具有更低能量消耗的第二运行模式中
-在所述主空气压缩机(3)中压缩第二数量的空气，所述第二数量的空气比第一数量的空气少，
-将来自所述低压塔(35)底部的第二数量的第一液氧流(70)引入所述侧冷凝器(26)中，所述第二数量比第一数量少，
-除所述第一液氧流(70)之外，将第二液氧流(73)供给至所述侧冷凝器(26)，
其特征在于：
-用于将来自所述低压塔(35)的中间点的中间液体(43)引入所述主冷凝器(36)的蒸发空间中的设备，
-用于将在所述主冷凝器(36)中产生的蒸汽引入所述低压塔(35)中的设备，
-冷凝器-蒸发器形式的附加冷凝器(37)，
-用于将氧流(66)从所述低压塔(35)的下层区域引入所述附加冷凝器(37)的蒸发空间中的设备，
-用于将至少一部分在附加冷凝器的蒸发空间中形成的气体作为上升蒸汽引入低压塔(35)中的设备，
-用于将在所述侧冷凝器(26)中蒸发的氧(71)引入所述主热交换器(32、33)中的设备，
-用于获得在所述主冷凝器(32、33)中加热的氧作为气氧产品(72)的设备，
-用于压缩来自所述蒸馏塔系统的第一氮流(44)的冷压缩机(45)，
-用于将至少一部分在所述冷压缩机(45)中压缩的氮引入所述附加冷凝器(37)的液化空间中的设备，和
-用于将至少一部分在所述附加冷凝器(37)中产生的液氮作为回流引入所述蒸馏系统的至少一个塔(34、35)中的设备，
并且其特征还在于如下设计的用于切换的设备，
在第一运行模式中
-在所述冷压缩机(45)中压缩第一数量的氮，
-将来自所述高压塔(34)的第一数量的气氮(41、42)引入所述主冷凝器(36)中，和
-在所述主空气压缩机(3)中将第一数量的空气压缩至第一总空气压力，以及
在第二运行模式中
-在所述冷压缩机(45)中压缩第二数量的氮，所述第二数量的氮多于第一数量的氮，
-将来自所述高压塔(34)的第二数量的气氮(41、42)引入所述主冷凝器(36)中，所述第二数量少于第一数量，和
-在所述主空气压缩机(3)中将第二数量的空气压缩至低于第一总空气压力的第二总空气压力。
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