CN1129793A - 用低温蒸馏法生产氧气的工艺和设备 - Google Patents

用低温蒸馏法生产氧气的工艺和设备 Download PDF

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CN1129793A
CN1129793A CN95117123A CN95117123A CN1129793A CN 1129793 A CN1129793 A CN 1129793A CN 95117123 A CN95117123 A CN 95117123A CN 95117123 A CN95117123 A CN 95117123A CN 1129793 A CN1129793 A CN 1129793A
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oxygen
pressure column
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Y·科伯尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

从混合气体中生产氧气的设备有一个双蒸馏塔(5)，通过从低压塔的底部蒸发出液氧的方法使混合气的一部分或全部在主冷凝器(8)中冷凝，其中从液相中分离出全部压缩成应用压力的气态氧气产品。冷凝器最好为流体逆流循环式热交换器。

Description

用低温蒸馏法生产氧气的工艺和设备
本发明涉及一种用空气蒸馏法生产氧气的工艺和设备，特别是生产不纯氧气，例如纯度至少为95％的氧气。
它涉及用空气蒸馏法在双塔中生产氧气的方法，双塔包括中压塔和低压塔，这些塔是通过两蒸发器/冷凝器互相进行热交换。主蒸发器在所供空气进入双塔之前冷凝空气的馏分，从低压塔底部蒸发出氧气。中间蒸发器通过从低压塔的中部蒸发液体来从中压塔顶部冷凝出氮气。
现有技术(US—A—3,113,854；US—A—3,210,951；JP—A—61—259077)描述的工艺具有一定的优点，即相对于传统的包括单一蒸发器的双塔，它减小了输送进入中压塔空气的压力及降低送入塔中的空气的压缩能量。
所用方法(US—A—3,210,951)包括将首先供入的空气馏分基本冷凝到中压塔的压力，从低压塔的底部蒸发出所有氧气，包括液态空气的产品被送入双塔，并且向中压塔提供冷却到露点的第二空气馏分。
另一方法(US—A—3,113,854)包括从低压塔底部蒸馏所有所供空气，以得到氧气，将它们部分冷凝并送入中压塔中，这种解决方案相对于前一方案的优点是：降低了空气冷凝的平均温度和由此产生的氧气压力，以此获得相对于前一工艺的压缩能量增加。在冷凝空气的第一馏分达到约37％时，中压塔的压力能降低到65Psia(4.5×105Pa)。系统所需的制冷量由氮涡轮机提供。
另一方法(JP—A—61—259077)也可得到在某种程度上相对于前一方法的空气的压缩能量增加，其主蒸发器只蒸发低压塔中再沸腾的氧气，从液相中提取产物。遗憾的是，所提供的空气不是被全部送到主蒸发器中。一部分空气通过膨胀阀送入中压塔的底部，这表明空气压缩的压力应比中压塔中的压力更高。在此条件下，送入主蒸发器的空气馏分比蒸发所有的氧气时冷凝得少些，但比利用所有空气时冷凝得要多些。
US—A—4,502518公开了一种低能量的在同一原理上生产高纯度氮和不纯氧的工艺方法。在约4巴下操作的低压塔底部部分冷凝中压空气，利用在低压塔底部生产的不纯氧气(20％N2)通过在低压塔顶部的冷凝器中低压蒸发来增加塔顶部的回流。
本发明的目的是相对于公知方法减少在压力下生产氧气方法中的能源消耗。
依照本发明，该方法为在一双塔中利用所供的含氧气和氮气的混合气体的低温蒸馏制备氧气。该双塔包括一中压塔和一低压塔，其中部分混合气被送入低压塔，所供混合气的至少一种馏分通过在低压塔底蒸发液氧，使其在冷凝器中部分冷凝，所述部分冷凝混合气被送入双塔，氧气从低压塔中分离出来。
低压塔在接近大气压力的压力下运行是较理想的。
将少于30％的所供混合气在冷凝之后送入中压塔中较为适宜，或最好是送入少于25％的混合气。
在冷凝器中部分冷凝中压塔中所有混合气或所供所有混合气体这一方法是有利的。
本发明还有一目的是提供一种从包含氧气和氮气的混合气中低温蒸发制备氧气的装置，它包括一个具有一个中压塔和一个低压塔的双塔，用于输送混合气的第一馏分到蒸发/冷凝器中的装置，适合通过与液态氧在低压塔的底部进行热交换，部分冷凝至少一部分混合气体，用于从低压塔底部提取氧气的装置，以及用于输送至少部分混合气的所述馏分到双塔中的装置。
低压塔可在常压下工作。
本发明的再一个目的是提供一种流动液体热交换器，它通过与至少部分冷凝的气体进行热交换而蒸发液体，其特征在于它包括使待蒸发的液体以与待冷凝的流体相反的方向在热交换通道内循环的装置。
现在将参照附图公开本发明的4个实施例。图1、2、3和4示意地示出了依照本发明的蒸馏空气装置的4个实施例。
如图1为一利用双塔5的方法，它的中压塔6仅为3.3×105帕，低压塔7为1.3×105帕。
待处理的空气被空气压缩机1压缩到3.5×105帕，在冷却到环境温度并纯化之后，空气被分成两部分100，101。
所供空气的第一馏分(62％)101通过主交换器3后输入蒸发/冷凝器8中，它构成双塔5的主蒸发器，该第一蒸发/冷凝器将所供空气的第二部分通过与包含在低压塔7底部的不纯氧热交换部分冷凝。一般地，仅第一馏分的18％被冷凝。部分冷凝气体通过导管104进到中压塔6的下部蒸馏。
压缩空气的第二部分100(38％)送入增压器102，然后在进入主交换器3之后被分为两路，一路由压缩空气的10％组成，它经部分冷却后送到涡轮机4(具有制动器204)，并使它膨胀到低压塔7的压力。
由压缩空气的28％组成的第二路在交换器3中冷却，然后在塔5外的辅蒸发/冷凝器115中通过与从低压塔7底部分离出的液态氧逆流热交换的方式全部冷凝，液氧由它的静压头加压。
不过，在所示实施例中，如果客户需要它能被泵126加压(由虚线表示)。冷凝空气分别通过各自导管116、117送入中和低压塔6，7中。
空气在中压塔6中分离，以在底部产生富氧液体的馏分，而在其顶部产生富氮气体。富化液体由导管105送入低压塔7之前在交换器103中过冷却。在送风引入点的高度上喷射富化液体。顶部气体通过导管109分离，并送入第二蒸发/冷凝器108中，在此它被冷凝，部分冷凝液体通过导管106回到中压塔5的上部，用作回流。冷凝液的另一部分在交换器103中过冷却后被喷入低压塔7的顶部以用作回流。
第二蒸发/冷凝器108可有效地冷凝上部的富氮气，因为其蒸发的液体只含80％的氧气。
依照本发明的设备，如图1所示，通过从液相中提取产品氧使中压塔的压力减小了，这会对空气的第一部分在低压塔7的底部蒸发器中的部分冷凝有很大影响，这部分空气是用于中压塔6的。从液相中产生的氧在应用压力下被蒸发，同时冷凝塔5外的全部第二部分空气。氧气的最大纯度为95％。
参阅图1的装置和US—A—3,113,854，送入中压塔的冷凝空气总量基本上是相同的，因为在图1中，冷凝空气的百分比大约为38％(＝28％＋62％的18％)，通过导管117送入低压塔7的冷凝空气量较少。
图1的系统允许进一步减小中压塔6的压力，因此也减少了压缩机1的输出压力。因为通过从辅助蒸发器115中提取液氧而使低压塔底部蒸发出的液氧数量减小，在蒸发器8中冷凝的空气减少，因而能在低温下进行，从而也在低压下进行。按照图1的实施例，利用辅助蒸发器使冷凝器1的工作压力由此降到3.5×105帕。因此，该压力是1.1×105帕，低于美国专利US—A—3,113,854的压缩机的压力。
此外，空气以低温状态离开压缩机，因此冷却系统的规模也相应减少。
本发明的方法允许在很低的比耗(0.25—0.30KW/Nm3纯氧之间)下生产氧气，消耗是氧气纯度的函数，是空气分离装置尺寸的函数。图1的实施例给出的能量为0.25kw/Nm3。
蒸发器8最好选用欧洲专利EP—A—130,122中公开的普通型，但需要时可用浴式蒸发器代替。
更好地，蒸发器8为流动液蒸发器，在此待蒸发液体(不纯氧)和待部分冷凝的气体(空气)沿相反的方向循环，也就是说逆流。这种类型的蒸发器最好为同流蒸发器，例如那些具有特定应用的欧洲专利申请EP—A—130122中的蒸发器，因为两种换热流体(空气和氧气)是不纯的，并在单一温度下不蒸发。逆流交换器的利用允许在此情况下减少不可逆性。
在依照本发明的装置的变型中，如图2所示，空气的第一部分在低压塔7的压力下在辅助塔206的底部冷凝器内部分冷凝，然后送入中压塔6中。辅助塔206从低压塔7的底部提供给它不纯液氧。
该变型允许在应用本发明时改变已使用的双塔。
在该变型中，增压空气(102)的第二部分冷凝，不是在独立的蒸发器中(如图1所示)而是在主交换器3中与由泵126泵入的液氧进行热交换。这些冷凝空气分别通过各自的导管116，117送入塔6，7中，这样所有用于蒸馏的空气不是在冷凝器8中部分冷凝就是全部冷凝。
设备所需的冷量由用于中压氮的膨胀涡轮机24提供和省略图1的吸气涡轮机。
在依照本发明装置的变型中，如图3所示，所有的空气在辅助塔206的主蒸发器中部分冷凝，然后送入中压塔6中。
在本变型中，从辅助塔中分离的液氧在热交换管路中蒸发，同时冷凝从中压塔上部来的经过再热并压缩到氧气的气化压力的气态氮，通过冷凝所获得的液氮返回到中压塔的顶部。
在本发明的另一变型中，如图4所示，装置的冷含量由所供空气的一部分在涡轮机中膨胀而得，该涡轮机与循环压缩器102相连，膨胀的空气被吸入低压塔中。

Claims (27)

1.一种在双塔〔5〕中用包含氧气和氮气的混合气通过低温蒸馏生产氧气的办法，该双塔〔5〕由中压塔〔6〕和低压塔〔7〕组成，其中将部分混合气送入低压塔〔7〕中，所供混合气的至少一种馏分在冷凝器〔8〕中被部分冷凝，它是通过蒸发来自低压塔〔7〕底部的液态氧进行的，所述部分冷凝混合气被送到双塔〔5〕，并从低压塔〔7〕中提取氧气。
2.根据权利要求1所述的方法，其中低压塔在常压下运行。
3.根据权利要求1或2所述的方法，其特征在于冷凝送入冷凝器〔8〕中的少于30％的所述混合气馏分。
4.根据权利要求3所述的方法，其特征在于冷凝送入冷凝器〔8〕中的少于25％的所述混合气馏分。
5.根据权利要求1到4所述的方法，其特征在于产品氧气在双塔〔5〕外的辅蒸发器〔115，3〕中蒸发。
6.根据权利要求5所述的方法，其特征在于辅蒸发器与交换器〔3〕合为一体。
7.根据权利要求5或6所述的方法，其特征在于利用所供混合气的第二馏分的全部冷凝，使产品氧气在液相下分离和蒸发〔115；3〕，利用氧的蒸发使它达到冷凝压力。
8.根据权利要求5或6所述的方法，其特征在于通过全部冷凝达到冷凝压力并被引入双塔〔5〕中的富有循环氮的混合气来蒸发出产品氧。
9.根据上述权利要求中任一项所述的方法，其中所有用于中压塔的所供混合气在冷凝器〔8〕中部分冷凝。
10.根据权利要求9所述的方法，其中所有所供混合气在冷凝器〔8〕中部分冷凝。
11.根据上述权利要求中任一项所述的方法，其中将形成气态产品的所有氧气是从低压塔底部的液相中提取的并达到应用压力。
12.根据上述任一权利要求所述的方法，其中部分冷凝所供混合气中至少一种馏分的冷凝器〔8〕是流动液氧热交换器。
13.根据权利要求12所述的方法，其中从低压塔底流出的液氧在热交换器〔8〕中沿与所供混合气相反的方向循环。
14.根据上述任一权利要求所述的方法，其中氧气产品的最大纯度为95％。
15.一种利用低温蒸馏包含氧和氮的混合气生产氧气的装置，它包括具有一个中压塔〔6〕和一个低压塔〔7〕的双塔〔5〕；用于将混合气的第一馏分送入冷凝器〔8〕中的装置，该冷凝器〔8〕适合于通过与来自低压塔〔7〕底部的液氧进行热交换来部分冷凝至少一部分所供混合气；用于从低压塔底部提取氧气的装置以及用于将至少一部所述混合气的馏分送到双塔〔5〕中的装置。
16.根据权利要求15所述的装置，其中低压塔〔7〕在大气压下运行。
17.根据权利要求15或16所述的装置，其特征在于它包括在双塔外的辅蒸发器/冷凝器〔115，3〕，适合于在液相中提取氧气。
18.根据权利要求17所述的装置，其特征在于辅蒸发器〔115.3〕是适于冷凝混合气的第二馏分或富氮混合气流，第二馏分或富氮的混合气流通过蒸发氧气来达到其冷凝压力。
19.根据权利要求15到18中任一项所述的装置，其特征在于冷凝器〔8〕设在辅助塔〔206〕中。
20.根据权利要求15到18中任一项所述的装置，其特征在于它包括一个两级压缩机〔1〕。
21.根据上述任一权利要求所述的装置，包括用于从低压塔〔7〕的底部以液相分离作为气体产品的所有氧气的装置。
22.根据上述任一权利要求所述的装置，其中冷凝器〔8〕是流动液氧热交换器。
23.根据权利要求22所述的装置，其中交换器允许在所供混合气和液氧之间进行热交换，并包括使液体与气体进行逆流循环的装置。
24.流动液体热交换器，通过与至少部分冷凝的气体进热交换来蒸发液体，其特征在于它包括用于使待蒸发的液体与待冷凝的气体在热交换通道中逆流循环的装置。
25.根据权利要求24所述的热交换器，其中液体和气体是不纯的。
26.根据权利要求25所述的热交换器，其中液体是不纯氧气，其最大纯度为95％，气体是空气。
27.一种以蒸馏形式分离空气的设备，包括在相对较高的压力下运行的第一蒸馏塔〔6〕，和一在相对较低的压力下运行的第二蒸馏塔〔7〕，和一热交换器(8)，它使来自第二塔底的液氧和至少一部分待蒸馏的空气之间进行热交换，其特征在于所述热交换器是权利要求24，25或26其中之一限定的热交换器，它包括用于给氧和空气提供热交换器通道的装置。
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