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CN1103041C - 制备低纯氧气的副塔低温精馏系统 - Google Patents

制备低纯氧气的副塔低温精馏系统 Download PDF

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CN1103041C
CN1103041C CN95102554A CN95102554A CN1103041C CN 1103041 C CN1103041 C CN 1103041C CN 95102554 A CN95102554 A CN 95102554A CN 95102554 A CN95102554 A CN 95102554A CN 1103041 C CN1103041 C CN 1103041C
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Abstract

本发明涉及用于制备低纯氧气的使用双塔和辅助的副塔的低温精馏系统，其中副塔通过要冷凝的压缩原料空气驱动，从而可使系统在较低压头下运行，因而降低了操作费用。

Description

制备低纯氧气的副塔低温精馏系统
本发明一般涉及低温精馏，更具体地说，涉及低纯氧气的制备。
空气的低温分离是一种良好设立的工业方法。低温空气分离包括将原料空气过滤以除去粒状物和将过滤后的原料空气压缩以提供分离所需的能量。压缩后从原料空气中除去诸如二氧化碳和水蒸汽等高沸点杂质并将其冷却，然后通过低温精馏分离出制品。分离塔在低温下运作以让气体和液体得以进行蒸馏分离所需的接触，然后将分离的制品逆着要冷却的原料空气流回到常温条件下。
用于氧气的制备的聚常用的低温空气分离系统是双塔系统，它使用一高压塔和一低压塔，两塔通过一主冷凝器进行热交换。在该系统中其压头就是在基础负荷空气压缩机的降压值，该降压值是由高压塔底部压力加上在管道及在基础负荷空气压缩机和高压塔间的设备的压降来定的。反过来，高压塔底部压力是由从低压塔顶到大气的气流的压降、由对低压塔底部附加的压差、由决定高压塔顶部高压氮冷凝压力的主冷凝器两端的温差，和由对高压塔底部附加的压降来定的。在常规系统中高压塔底部压力一般在70到80磅/平方英寸(绝对值)(psia)范围内，因而使压力一般在77到89psia范围内。
用常规双塔系统进行空气分离可获得良好的能效和优异的产品纯度。但是如果需要低纯氧气即纯度在99(mol)％或以下的氧气，那末常规系统的效率是较低的，因为只有一部分空气分离能力得到了利用。因为在诸如玻璃制造、炼钢和能源生产等应用中对低纯氧气的需要日益增加，因此需要可以低运行费用从生产低纯氧气的双塔系统。
因此，本发明的一个目的是提供制备低纯氧气的改良双塔低温精馏系统。
通过本发明便可达到上述和其他目的，这些目的对本领域技术人员来说一旦读了本公开后就变得显而易见，本发明的一个方面是：
制备低纯氧的低温精馏方法，它包括：
(A)压缩原料空气；
(B)将压缩的原料空气至少部分地冷凝，并将这样得到的原料空气送到也包括低塔的双塔的高压塔中；
(C)将含有55-80(mol)％氧气的粗制液氧从低压塔输送到副塔中；
(D)通过在副塔内的低温精馏将粗制液氧分离成氧制品流体和残余蒸汽；
(E)将残余蒸汽从副塔送到低压塔中；
(F)通过和压缩的原料空气间接热交热将氧制品液至少部分地气化，并将压缩的原料空气进行所述的至少部分的冷凝；和
(G)回收含氧气量超过粗制液态氧气的作为产品低纯氧气的氧气制品流体。
本发明的另一方面是：
低温精馏设备，它包括：
(A)基础负荷原料空气压缩器；
(B)具有底部再沸器的副塔；
(C)包括第一塔和第二塔的双塔；
(D)将原料空气从基础负荷原料空气压缩器送到底部再沸器和从底部再沸器送到第一塔的装置；
(E)将流体从第二塔的下部送到副塔的装置；
(F)将流体从副塔送到第二塔的装置；和
(G)从副塔回收制品的装置。
这里所述的术语“塔”是指蒸馏塔或蒸馏区、或分馏塔成分馏区，即接触塔或接触区，其中液相和气相逆流接触而使流体混合物分离，例如通过在塔内安的一系列重直分隔的塔板或片上和/或在诸如有规则填充物或无规填充物上进行气液相的接触而使混合物分离。关于蒸馏的进一步讨论，可能见R.H.Perry和C.H.Chilton编的《化学工程师手册》第五版的13部分：连续蒸馏方法，出版商为纽约的Mc Graw-Hill Book Company。术语双塔是指其上端和低压塔的下端具有热交换关系的高压塔。关于双塔的进一步讨论可参见1949年牛津大学出版社Ruheman的《气体分离)》一书的第六章：商业空气分离。
气液接触分离方法取决于组分蒸汽压力的不同。高蒸汽压(或易挥发或低沸点)组分趋于富集在气相中，而低蒸汽压(或难挥发或高沸点)组分则趋于富集在液相中。部分冷凝是将气态混合物冷却以将挥发性组分富集于气相而将难挥发组分富集于液相中的分离过程。精馏或连续蒸馏是通过对气相和液相逆流处理获得的、结合连续部分汽化和冷凝的分离过程。气相和液相的逆流接触一般是绝热的，可包括相间的积分(分阶段的)接触或微分(连续)接触。利用精馏分离混合物的原理进行分离处理的配置通常可交替地称为精馏塔、蒸馏塔或分馏塔。低温精馏是至少部发在开氏150度(°K)或以下温度进行的精馏过程。
这里所用的术语“间接热交换”是指两种流体在没有任何物理接触或流体间的相互混合的情况下进行的热交换。
这里所用的术语“底部再沸器”是指从塔底液中产生塔的上流蒸汽的热交换装置。
这里所用的术语“涡轮膨胀”和“涡轮聚冷器”各指高压气体流过涡轮机以降低气体的压力和温度从而产生致冷作用的方法和装置。
这里所用的术语“上部分”和“下部分”是各指在塔的中部上面和下面的部分。
这里所用的术语“原料空气”是指诸如周围空气等主要包含氮气和氧气的混合物。
这里所用的术语“低纯氧气”是指氧浓度在99(mol)％或以下的流体。
图1是本发明低温精馏系统的一个优选实施方案的图示。
图2是本发明的另一个优选实施方案的示意图，其中可制备较高压力的氧气制品。
图3是本发明的又一种优选实施方案的示意图，其中原料空气是在两个压力水平下提供给高压塔的。
图4是使用增压进料涡轮机的本发明的再一种优选方案的示意图
一般来说，通过将氧气制品的纯度对高压塔底部压力的相依性脱开，本发明可使双塔系统中的高压塔在较低压力下运作。这样本发明就可通过降低要获得必要的压头所需的原料空气压缩功来达到节省能量的目的。
本发明将根据附图来详细叙述。
现在参见图1，原料空气24通过在基础负荷原料空气压缩机25上将其压缩到一般在38至65psia的压力范围，然后通过冷却器26冷却以除去压缩热。此后将加压的原料空气27通过净化器28清除诸如水蒸气和二氧化碳待高沸点杂质，这样处理后的原料空气流1通过和在主热交换器70的返回流体间接热交换而冷却。一般占总原料空气百分之十到二十五的小部分(原料空气)2通过涡轮骤冷器80，涡轮膨胀而产生致冷并通过热交换器71进一步冷却，然后送到低压塔200中。
一般含百分之七十五至九十原料空气的部分3通过一般位于副塔300下部的底部再沸器350。在底部再沸器350内，经压缩的原料空气至少部分地被冷凝，此后这样得到的原料空气流29通过阀50送到高压塔100中。
高压塔100是双塔的第一塔或高压塔，双塔也包括第二塔或低压塔200。高压塔100的操作压力一般在30到60psia的范围内。在高压塔100内，原料空气通过低温精馏而分离成富氮蒸汽和富氧液体。富氮蒸汽流4通到主冷凝器250中通过和低压塔200底液间接热交换而冷凝。得到的富氮液31被分成液流6和5。液流6作为回流通到塔100中，液流5通过热交换器72冷冻并作为回流通过阀52通到塔200中。富氧液体作为液流7从塔100的下部导出并经热交换器73冷却，然后通过阀51送到塔200中。塔200的操作压力低于塔100，一般在16到25psia的范围内。主冷凝器250可以是常规的热虹吸装置，或可以是单程液体流装置，也可以是下流液体流装置。
在低压塔200内，进入该塔的各种原料通过低温精馏分离成富氮蒸汽和粗制液态氧。富氮蒸汽作为气流8从塔200的上部导出，通过热交换器72、73和70加温，然后作为气流33从系统中排出，它可作为废气排到大气中，也可全部或部分回收。气流33一般含氧气范围为0.1-2.5(mol)％而其余的基本上都是氮气。氧浓度范围为50-88(mol)％的粗制液氧从第二塔或低压塔200的下部导出并作为液流10通过副塔300的上部。
副塔的操作压力与低压塔200相似，一般在16到25psia的范围内。在副塔300内，下行的粗制液态氧通过逆着上流蒸汽的低温粗馏而加浓成氧气制品流体和其它的蒸汽。一般含氧25-65(mol)％含氮30-79(mol)％的其它蒸汽流13从副塔300的上部通到低压塔200中。
氧浓度超过粗制液态氧、含量范围达到70-99(mol)％的氧气制品流体作为流体在副塔300的下部收集其至少一部分通过和逆行的要冷凝的压缩原料空气在底部再沸器350中间接热交换而气化，再沸器350可以是常规的热虹吸装置或单程或下流型装置。这种气化可为粗制液氧在副塔300内的分离产生上流蒸汽。氧气制品流体可作为气体和/或液体回收。氧气制品气可作为气流11从副塔300导出、通过热交换器71和70加温并作为氧气制品气34回收。氧气制品液可作为液流12通过阀53从副塔300导出并作为氧气制品液35回收。氧气制品流体的氧气浓度在77-99(mol)％的范围内。
表1列出了通过计算机进行本发明的模拟来执行图1所示的实施方案所获的结果。在表1中各气液流的编号与图1相对应。提供本发明的这个实施例的目的是说明情况而不是对本发明的范围作限制。在该实施例中，高压塔含有20个理论塔板，低压塔含22个理论塔板，而副塔含8个理论塔板。
                         表1气液流    流速      压力      温度    组成(摩尔百分比)
      (lb.编号   mol/hr.)   (psia)    (°K)    N2   Ar     O21      100        60       289     78    0.9    20.92      9.8        59.4     139     78    0.9    20.93      90.2       57.4     95      78    0.9    20.97      62.2       55.9     94      68.5  1.2    30.310     33         18.3     89      13.6  3.4    8311     21.3       18.4     92      1.9   3.1    9512     0.1        18.4     92      0.5   2.1    97.413     11.6       18.3     89      35.2  3.8    61
在该实施例，氧气回收率是原料空气中所含氧气的97％。在该实施例中进行低温精馏所需的压头只有64psia。这比驱动相应的常规双塔分离所需的78psia低约18％，因而证明本发明的实施可获得良好的效果。
图2，3和4说明了本发明的其它优选的实施方案。对于普通组件在图2，3和4中的数码相应于图1的数码，这些普通组件将不再详细讨论。
现在参照图2，原料空气流1的一部分36通过压缩机37进一步压缩，通过冷凝器38冷却压缩热并作为气流30通过主热交换器70和阀56，在原料空气流29导入塔100的进口的上方导入高压塔100中。氧气制品液流12通过液体泵60提高压力，加压后的液流14通过主热交换器70气化而制备出升高压力的低纯氧气制品气流15。一般所述升高压力的氧气制品气的压力在30至300psia范围内。依照热交换器设计需要，最好与要冷凝的气流30相逆向的液流14的煮沸在单独的位于液体泵60和主热交换器70之间的热交换器(未画出)中进行。
在图3所说明的实施方案中，原料空气1的一部分20在通过主热交换器70和底部再沸器350前径压缩机39进一步压缩，而原料空气流的其余部分32通过主热交换器70但绕过底部再沸器350而直接通入塔100中。该实施方案可使人们更容易将要通过底部再沸器350的原料空气全部冷凝，当要制备氧气纯度在90-99(mol)％内的氧气制品时这是有利的。
在图4说明的实施方案中，一部分原料空气2取自气流1中主热交换器70的上游并通过压缩机90压缩。压缩后的气流通过冷凝器91冷却以除去压缩热并部分地通过主热交换器70。此后该气流通过涡轮骤冷器80涡轮膨胀而产生致冷并由此通过热交换器71进入低压塔200。涡轮骤冷器80直接和压缩机90匹配以便让通过经涡轮骤冷器80的加压的气体流2的膨胀释放的能量来驱动压缩机90。该实施方案从设备的观点出发是好的，它也可用于制备氧气纯度在90-99(mol)％范围内的氧气制品。
因此通过本发明的应用，人们可以用双塔在较低的压力下有效地制备低纯氧气，而降低常规的双塔系统所需的费用。尽管经根据一定的优选的实施方案详细描述了本发明的情况，本领域技术人员会认识到本权利要求书的精神和范围内还有本发明的其它实施方案。

Claims (8)

1.制备低纯氧气的低温精馏方法，包括
(A)压缩原料空气；
(B)将压缩的原料空气至少部分地冷凝，并将这样得到的原料空气送到也包括低压塔的双塔的高压塔中；
(C)将一小部分压缩的原料空气经涡轮膨胀而致冷；
(D)将含有55-80(mole)％氧气的粗制液氧从低压塔输送到副塔中；
(E)通过在副塔内的低温精馏将粗制液氧分离成氧制品流体和其它蒸汽；
(F)将其它蒸汽从副塔送到低压塔中；
(G)通过和压缩的原料空气间接热交换使氧制品液至少部分地气化，并将压缩的原料空气进行所述的至少部分的冷凝；和
(H)回收含氧气量超过粗制液态氧气作为产品低纯氧气的氧气制品流体。
2.权利要求1的方法，其中氧气制品流体是以气体回收的。
3.权利要求1的方法，其中氧气制品流体是以液体回收的。
4.权利要求1的方法，其中氧气制品流体以液态从副塔导出、并增压、在回收前先气化。
5.权利要求1的方法，还包括将一部分经压缩的原料空气涡轮膨胀，并将经涡轮膨胀的原料空气送到低压塔中。
6.低温精馏设备，包括基础负荷原料空气压缩机和包括第一塔和第二塔的双塔，其特征在于进一步包括：
具有底部再沸器的副塔；
将原料空气从基础负荷原料空气压缩机送到底部再沸器和从底部再沸器送到第一塔的装置；
将流体从第二塔的下部送到副塔的装置；
将流体从副塔送到第二塔的装置；
从副塔回收制品的装置；和
涡轮膨胀器、将原料空气送到涡轮膨胀器的装置、和将原料空气从涡轮膨胀器送到第二塔的装置。
7.权利要求6的设备，其中从副塔回收制品的装置包括液体泵。
8.权利要求6的设备，还包括与涡轮膨胀器直接匹配的压缩机，其中将原料空气送到涡轮膨胀器的装置包括从所述的直接匹配的压缩机到涡轮膨胀器的导管装置。
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