CN1097716C - 低温蒸馏分离气体混合物的方法和装置 - Google Patents

低温蒸馏分离气体混合物的方法和装置 Download PDF

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CN1097716C
CN1097716C CN95104710A CN95104710A CN1097716C CN 1097716 C CN1097716 C CN 1097716C CN 95104710 A CN95104710 A CN 95104710A CN 95104710 A CN95104710 A CN 95104710A CN 1097716 C CN1097716 C CN 1097716C
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N·里思
B·达雷德奥
J-Y·莱曼
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

为了使装有结构填料的蒸馏装置(15)的产量提高到高于额定产量的值，本发明提供了装置(1、3)以提高该装置的操作压力从而提高相同尺寸的装置液泛的极限。主热交换器(9)的通道分配可以根据已确定的生产方式改变。

Description

低温蒸馏分离气体混合物的方法和装置
本发明涉及一种采用低温蒸馏混合物以生产不同流量的至少一种纯组分的装置。本发明首先涉及一种额定生产的装置，并可从额定产量转变到最大产量，从而使产量比额定产量大大地增加。
在已知的这种空气蒸馏装置中，构成该装置的部件都是超尺寸的且其生产量降低，其降低程度可达最大产量的40％。很明显，按100％的生产能力进行操作而设计的装置，其功能仅及该生产能力的60％必然是不经济的。
在没有超尺寸的板式塔中，只允许流量超过5-10％。超出此值，塔径和板间距都必须超尺寸才有可能使流量超过10％。
本发明的目的在于提供一种设计成不仅可以在额定产量下尽可能增加产量而且还适合于在只需作最少的技术改进后即能在高于额定产量的生产能力下操作的装置。
为此，本发明的目的在于提供一种在蒸馏装置中分馏混合物以生产不同流量的至少一种纯组分的装置，所述蒸馏装置主要装有填料结构，并按在额定压力下处理额定流量的所述混合物确定尺寸，其特征在于为了获得比额定产量更高的产量，该装置包括一些设备，这些设备可以增加该装置中待蒸馏混合物的流量从而相应提高产量，此外，还包括一些可以提高该装置的操作压力以便提高该装置的液泛极限的设备。
该填料可以是交叉—波纹型(cross-corrugation)。
该装置中待蒸馏的混合物可以是空气。
为纯化待分离的原料料流例如空气，安装了一台逆流吸附塔，该吸附塔可以用蒸馏装置中排出的废气流再生，而且在该废气的流量明显低于所述装置在额定条件下操作时所产生的废气的额定流量下，该吸附塔可以有效地再生。
该装置还包括一套热交换系统，其中待分馏混合物与该装置中的至少一种产品之间发生间接热交换，从而使待分馏的混合物冷却而使所述至少一种产品再加热。该热交换系统按额定产量定尺寸。通道数之间的分配比例最好根据已确定的生产方式改变。
因此，当产量大于额定产量时，与额定产量下分配的通道数相比，分配给该装置中至少一种产品的通道数相对减少，这样，即可将腾出的通道分配给待分馏的混合物或该装置中至少一种其它的产品。
例如，当待分馏的混合物是空气，其产量大于额定产量时，可将分配给残余氮的通道数减少。
本发明的目的还在于提供一种提高装置生产率的方法，该装置用于在蒸馏装置中分馏混合物以生产至少一种纯组分，其中蒸馏装置主要装有结构填料，按处理所述混合物的额定流量确定其尺寸，并可从额定产量转变到较高的产量，
i)根据所述的生产比例，待分馏混合物的流量明显提高，和
ii)同时，该装置的分馏压力增高，足以提高该装置的液泛极限。
本发明的目的还在于提供一种提高装置生产率的方法，该装置用于通过蒸馏生产至少一种纯组分，该装置包括具有许多分配给待再加热和待冷却流体的通道的热交换器，其特征在于可以根据该装置产量的变化改变通道的分配。
当装置的产量增加时，最好增加分配给待冷却流体的通道数，使分配给待再加热流体的通道数减少。
具体地说，待冷却的流体将进行蒸馏，而待再加热的流体是蒸馏产品。
在最大的产量下，可以增加分配给待蒸馏流体的通道数，而将分配给蒸馏的残余气体的通道数减少。
现在，参照附图列举出本发明的操作实施例，其中：
—图1是根据本发明装置的一个实施方案的示意图；和
—图2是图1中热交换系统的一部分示意图。
图1的装置主要包括鼓风机1、主空气压缩机3、制冷组5、吸附纯化装置7、热交换系统9、与空气压缩机13配合的供冷透平机11、由包括中压塔(MP)15A和装在顶部的低压塔(LP)15B的双层塔构成的蒸馏装置15、该双层塔装有填料结构17、再生式再加热器19、氮气压缩机21以及氧气压缩机23。
为了叙述该装置的操作，首先假定它是在额定产量(每天480吨)下生产氧。在此情况下，空气鼓风机1不运行，而额定流量的空气仅通过压缩机3压缩到5×105Pa，冷却到室温，在装置7中纯化，然后分成两股气流。一股气流在送进中压塔15A的底部之前，被直接输送到热交换系统9，在其中于5×105Pa下冷却到接近其露点。另一股气流通过压缩机13压缩，在热交换系统9中部分冷却，在透平机11中膨胀，然后被送到低压塔15B。
来自中压塔15A底部的富液被膨胀到105Pa，然后送到低压塔15B的中部，来自中压塔15A顶部的贫液被膨胀到105Pa，然后送到低压塔15B的顶部。
从低压塔15B排出的不纯氮气流在热交换系统9中再加热，根据具体情况在再加热器19中再加热后，送到纯化装置7再生。
氧气流从低压塔15B的底部排出，然后通过热交换系统9，在其中被低压塔15B顶部排出的氮气流再加热。然后，分别通过压缩机21和23将该氮气和氧气压缩。
为了使该装置能在氧的额定产量的130％(每天620吨)下操作，启动鼓风机1，该鼓风机的体积流量大体与压缩机3适应，并可按其输出功率供给接近该产率的1.3×105Pa的压力。这样，压缩机3(按其在额定生产能力下操作定尺寸)当其进气压力等于大气压时(连续处理恒定体积流量时)也能在重量流量增加的情况下操作。因此，可以保证压缩机3的进气流量恒定，使供入空气的压力升高到6.5×105Pa。
制冷组5按最大产量(额定产量的130％)定尺寸；然而，空气纯化装置7却按额定产量定尺寸。当供入空气的流量增加到其最大值时，空气中所含的CO2流量成比例地增加，因此，为了吸收所有的CO2，同时确保在再加热器19中加热的再生流量不超过额定产量的再生流量的20％，该装置的循环时间减少约11％。
                         表1
  每天480吨(图1)   每天620吨(图1)
槽压(106Paa)     5.26     6.4
待纯化空气的温度℃     10     10
空气流量(Nm3/h)     68,660     89,196
水流量(kg/h)     131     141
CO2流量(kg/h)     54     70
循环时间(min)     180     160
再生流量(Nm3/h)     11,404     13,677
由于塔15中装有结构填料17，当达到最大产量时，按接近生产能力增加的比例增加压力，可以保持体积流量。在上述装有结构填料的条件下未遇到″过滤″现象，这是因为该填料可以支承大于额定生产能力30-50％的液体负荷。然而，多孔板却不如此，其板间距和液体流道不可能处理超过其设计值的流量。
                                 表2
按每天480吨生产   增加到每天620吨
中压塔压头(105Paa)     4.92     6.07
低压塔压力(105Paa)     1.35     1.72
低压塔底部气体流量(Nm3/h)     36,372     47,192
中压塔顶部气体流量(Nm3/h)     69,339     91,974
表2说明，塔中的体积流量几乎可以保持恒定，主要是由于其中装有结构填料所致。
塔15明显具有在最大产量时能耐压力增加的壁厚。
压缩机21和23比额定值稍超尺寸，在最大产量下也可以输出所需的压力。
作为一种变型，可以取消鼓风机1，而压缩机3则按操作的极端条件定尺寸。
在上述条件下，通过调节压缩机进口处的可变叶片，该装置可以连续地从额定产量改变为最大产量。
最后，对于图1的这种在双层塔中蒸馏空气的装置而言，该压缩空气的压力是下列各项的函数：蒸馏过程中被分离产品的出口压力、这些产品在热交换系统中和纯化残余氮的再生过程中的压力损失、主汽化器中的温度差、塔中的压力损失以及在热交换系统中空气产生的压力损失。在低压塔中，存在临界产量(与施加的出口压力以及热交换系统和低压塔中的压力降有关)，它决定下列压力：
—低压塔底部也就是说在主汽化器中的最低压力，因而是在中压塔顶部氮的冷凝压力(与中压塔中的压力降和热交换系统中空气的压力降有关)，
—空气压缩机的输送压力。
在最大产量下，为了尽量避开液泛极限运行，必须使塔的压力升高得比输出产品的压力降更快，因此，可以增加非商品的产品例如不纯氮的压力降，这样，它的压力足以在常压下再生吸附剂。上述压力降的增加可以通过减少残余氮的通道数以利于增加空气的通道数(使其压力降减少)。在固定的蒸馏压力下，空气压缩机(具有较低的出口压力)的能量降低。
然而，根据所需产品的类型，其它通道的再分配显然是有价值的。
因此，如果分配给残余氮的通道数减少到最大程度，如上所述，可将空闲的通道分配给另一种产品或在热交换系统中再加热的其它蒸馏产品，而不是将其分配给空气。这样，在压力降减小的条件下，可以提高至少一种其它蒸馏产品的出口压力。
需要特别指出的是，热交换系统通道的这种再分配的方法可以应用于除空气蒸馏装置外的其它的装置。
根据图2，操作条件的改变是通过板式热交换器类型的热交换系统9中的流体再分配而实现的。图1中，在后者的上部可以看到两个流体进口和三个出口。仅对四个热交换器9的机体之一作了说明。供入的空气处于两种压力(HP、MP)，来自压缩机13的空气处于高压(HP)，而直接来自纯化器7的是中压空气(MP)。在额定的条件下，该空气与来自低压塔15B的氧气流、来自低压塔15B顶部的氮气流以及再生纯化装置7的残余氮气流逆流而被冷却。后述的这些流体则被再加热。
在额定产量的情况下，中压(MP)空气在热交换器9的每个机体上被分配最多48个通道，其压力降为200mbar，而残余氮被分配最多30个通道，其压力降为94mbar(参阅表3和表4)。
在最大产量下，中压空气流过11个在额定产量下被残余氮通过的通道，该空气的压力降降低到186mbar，而没有进行热交换但是通过19个通道的残余氮的压力降则升高到259mbar。
在最大产量时，随着供入的空气以及原有产品的压力升高，对于将进入大气中的残余氮而言在管中较大的压力降是可以容许的，对构成系统中所有回收压能的空气而言，在管中压力降较小。
                           表3：热交换系统(每天480吨)
    MP空气    HP空气     LPGN     GO     RN
 Q总Nm3/h     63,100     3,500     25,000     14,013     27,587
 Q/机体Nm3/h     15,775     875     8,250     3,503     6,897
 通道数/机体     48     8     32     14     30
 Q/通道/机体     329     109     195     250     230
 压力105Pa     5.156     7.069     1.257     1.354     1.255
 压力降(mbar)     200     21     70     117     94
注：MP、HP、LPGN、GO、RN分别代表中压、高压、低压气体氮、气体氧、残余氮(下同)
                                     表4：热交换系统(增加到每天620吨)
    MP空气    MP空气    HP空气    LPGN   GO   RN
  Q总Nm3/h     67,591    15,489     3,500    33,000   18,200   35,380
  Q/机体Nm3/h     16,898    3,872     875    8,250   4,550   8,845
  通道数     48    11     8    32   14   19
  Q/通道/机体     352    352     109    258   325   466
  压力105Pa     6.291    6.291     9.070    1.015   1.718   1.614
  压力降(mbar)     186    186     16    90   147   269

Claims (10)

1.用于在蒸馏装置(15)中通过分馏混合物生产不同流量的至少一种纯组分的装置，所述蒸馏装置主要包括结构填料(17)，并按在额定压力下处理额定流量的所述混合物确定尺寸，
其特征在于为了获得比额定产量更高的产量，该装置包括一些设备，这些设备可以增加该装置(15)中待蒸馏混合物的流量从而相应提高产量，此外，还包括一些可以提高该装置的操作压力以便提高该装置的液泛极限的设备。
2.根据权利要求1的装置，其中该混合物是空气。
3.根据权利要求1或2的装置，其中增加装置(15)中待蒸馏混合物流量的设备包括按额定生产能力设计的用于待分馏混合物的压缩机和在该压缩机上游的一台鼓风机(1)。
4.根据权利要求1或2的装置，其中增加装置(15)中待蒸馏混合物流量的设备包括按最大生产能力设计的用于待分馏混合物的压缩机(3)。
5.根据权利要求1的装置，该装置包括为纯化待分离的原料料流而安装的一台逆流吸附塔(7)，该吸附塔可以用蒸馏装置(15)中排出的废气流再生，而且在该废气的流量明显低于所述装置在额定条件下操作时所产生的废气的额定流量下，该吸附塔可以有效地再生。
6.根据权利要求1的装置，该装置包括一套热交换系统(9)，其中待分馏混合物与该装置(15)中的至少一种产品之间发生间接热交换，从而使待分馏的混合物冷却而使所述至少一种产品再加热，该热交换系统按额定产量设计，分配给该装置中的一种产品的通道数和分配给该装置中的至少一种其它产品的通道数之间的分配比例可根据生产方式改变。
7.根据权利要求1的装置，该装置包括一套热交换系统(9)，其中待分馏混合物与该装置中的一些产品之间发生间接热交换，从而使待分馏的混合物冷却而使所述至少一种产品再加热，该热交换系统按额定产量设计，分配给该装置中的一种产品的通道数和分配给该装置中的至少一种其它产品的通道数之间的分配比例可根据生产方式改变。
8.根据权利要求6或7的装置，其中当产量大于额定产量时，与额定产量下分配的通道数相比，分配给该装置中至少一种产品的通道数相对减少，这样，即可将腾出的通道分配给待分馏的混合物或装置(15)中至少一种其它的产品。
9.根据权利要求6或7的装置，其中待分馏的混合物是空气，该装置(15)产生残余氮，当产量大于额定产量时，将分配给残余氮的热交换系统(9)的通道数减少。
10.一种提高装置生产率的方法，该装置用于在蒸馏装置(15)中分馏混合物以生产至少一种纯组分，其中蒸馏装置(15)主要装有结构填料(17)，并按处理所述混合物的额定流量设计，其中可从额定产量转变到较高的产量，
i)根据所述的生产比例，待分馏混合物的流量明显提高，和
ii)同时，该装置(15)的分馏压力增高，足以提高该装置的液泛极限。
CN95104710A 1994-04-22 1995-04-21 低温蒸馏分离气体混合物的方法和装置 Expired - Fee Related CN1097716C (zh)

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