CN1071444C - 生产气体氧的低温空气分离*** - Google Patents

生产气体氧的低温空气分离*** Download PDF

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CN1071444C
CN1071444C CN93101820A CN93101820A CN1071444C CN 1071444 C CN1071444 C CN 1071444C CN 93101820 A CN93101820 A CN 93101820A CN 93101820 A CN93101820 A CN 93101820A CN 1071444 C CN1071444 C CN 1071444C
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liquid
air
oxygen
product generator
cryogenic rectification
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CN1075796A (zh
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J·R·德雷
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Praxair Technology Inc
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Abstract

一种采用结合有液态空气源的产品发生器的深冷空气分离***，借以使液态氧有效地汽化产生气态氧，同时使所说的深冷空气分离设备在稳态下运行而不招致明显的致冷作用损失。

Description

生产气体氧的低温空气分离***
本发明涉及低温或深冷空气分离领域，具体讲涉及生产气体氧产品的低温或深冷空气分离。
当某具体用途需要大量气体氧时，利用在低温精馏设备中对空气进行低温精馏的方法生产气体氧，并将其从所说设备直接用管道输送到使用地点。空气分离设备被设计成在某个稳态条件下以最有效的方式运行。但是，不同的使用场所可能需要数量不同的气体氧来满足各种状态下的要求。
为了适应深冷精馏设备的有效而稳态运行的要求和与之相矛盾的不同使用场所对气体氧需要量的各种要求，人们在淡季期采用气体氧贮罐来贮存所生产的气体氧，而在需求量大的时期可以将气体氧从氧贮罐放出送到所用地点，用这种方法来减缓深冷空气分离设备在运行速率上的波动，从而保持所说设备处于高运行效率之下。这种***的一个问题是：即使在高压下贮存气体氧，以这种方式也仅仅可以贮存有限量的气体氧而不占用需要很高投资费的气体氧贮罐用地。
以液体而不是以气体形态贮存氧，可以克服备用氧贮存量受限制的缺点。但是，这种方法虽然解决了贮存量有限的缺点，但是却有其自身的问题。一个问题是当将过量氧从深冷精馏设备以液态取出送入贮存罐时，该设备有很大的制冷损失；另一个问题是为了维持贮存的氧处于液态，需要向所说***中输入能量，但是在充分绝热的贮罐中此问题相当次要。还有一个问题是需要输入额外的能量来使液态氧汽化成气体氧产品。
因此，本发明目的在于提供一种用改进的深冷精馏***生产气体氧，这种***能更充分地利用液态氧贮存方法来减轻或缓和深冷精馏设备运行速率上的变化，同时还能满足对气体氧产品用量波动很大的要求。
本领域中普通技术人员阅读本说明书后显然明白本发明的上述目的和其它目的，本发明的内容之一是：
一种通过深冷精馏原料空气生产气体氧的方法，包括：
(A)将原料空气通入产品发生器中，与所说产品发生器中的液态氧进行间接热交换后冷凝进料空气；
(B)将冷凝的原料空气通入深冷精馏设备中生产液态氧；
(C)将在深冷精馏设备中生产的液态氧送入产品发生器中，以便进行原料空气的冷凝，并从产品发生器中回收气体氧产品；
(D)将在深冷精馏设备中生产的液态氧送入液氧贮罐，以生产储备的液态氧；
(E)利用从液氧贮罐向产品发生器中通入液氧，增大向产品发生器输送液氧的流量，同时相应增大原料空气向产品发生器中的流量，以生产过量的冷凝原料空气；以及
(F)将过量的冷凝原料空气送入液态空气贮罐，以生产储备的液态空气。
本发明的另一内容包括：
一种生产气体氧的深冷空气分离设备，包括：
(A)产品发生器、向产品发生器供给原料空气的装置和从产品发生器向深冷精馏设备输送液体的装置；
(B)从深泠精馏设备向产品发生器输送液体的装置和从产品发生器回收气体产品的装置；
(C)液氧贮罐、从深冷精馏设备向液氧贮罐输送液体的装置和从液氧贮罐向产品发生器输送液体的装置；
(D)液体空气贮罐、从产品发生器向液体空气贮罐输送液体的装置和从液体空气贮罐向深冷精馏设备输送液体的装置。
本文中使用的术语“产品发生器”，是指其中利用间接热交换使液氧沸腾，同时使空气蒸汽冷凝的一种热交换器。
本文中使用的术语“塔”，是指蒸馏或精馏塔或区，即其中液相或汽相对流接触实现流体混合物分离的接触塔或区，例如以装在所说塔中的一系列垂直相间的塔板或塔盘上，和/或在可以为有序和/或随机填充料的填充元件上使汽相和液相接触方式接触。有关蒸馏塔的详细讨论，参见<化学工程师手册>(第五版，R.H.Perry和C.H.Chilton编，McGraw-Hill图书公司，纽约)第13册中，由D.D.Smith等人撰写的“蒸馏”部分3-13页上的“连续蒸馏过程”。使用术语“双塔”是指按热交换关系使高压塔的上端与低压塔的下端相连；有关双塔的详细介绍参见Ruheman著<气体的分离>(牛津大学出版社，1949年)第Ⅶ章“空气的工业分离”。
蒸汽和液体的接触离过程，取决于诸成分的蒸气压差。高蒸气压(或易挥发或低沸点)成分易于在气相中富集，而低蒸气压(或难挥发或高沸点)成分易于在液相中富集。蒸馏是能够采用加热液体混合物在气相中富集易挥发成分、在液相中富集难挥发成分的分离过程。部分冷凝是能够利用冷却蒸汽混合物在气相中富集挥发性成分并在液相中富集难挥发成分的分离过程。精馏或连续蒸馏，是将通过对流处理气相和液相而产生的连续部分汽化和冷凝结合起来的分离过程。气相和液相的对流接触是绝热的，而且可以包括相之间的整体接触或微分接触。利用精馏分离混合物原理的分离过程设备，常常可以改称作精馏塔、蒸馏塔或分馏塔。深冷精馏，是一种至少部分在低温下，例如在等于或低于125°K温度下进行的精馏过程。
本申请使用的术语“间接热交换”，指使两种液流热交换而无液流间的互相物理接触或混合。
本中请使用的术语“氩塔”是指一种包含塔和顶部冷凝器的***，它处理含氩原料气并且生产氩浓度高于原料气中的产品。
唯一的附图是本发明深冷精馏***中一种优选方案的示意图，其中深冷精馏设备包括一个双塔及与之结合的氩塔。
本发明一般包括采用产品发生器来从液氧有效地产生气体氧，同时在产品发生器和深冷精馏设备间使用液体空气贮罐来同时减少从深冷精馏设备放出液氧引起的致冷损失和减缓操作速率波动的影响。
以下参照附图详细说明本发明。参看附图，将除去CO2和水蒸汽等低沸点杂质后的原料空气100通入热交换器101，用回流液间接热交换法冷却之。部分原料空气113用部分通过热交换器112的方法冷凝后，作为物流720的一部分被通入深冷空气分离设备之中；另一部分原料空气120被热交换器122中的氩产品冷凝后，被通入深冷精馏设备的塔中。第三部分原料空气103经过膨胀器102被膨胀产生致冷作用，并将生成的膨胀物流104像其它两部分原料空气那样通入空气分离设备的塔105之中。
将占原料空气100流量10-50％的部分原料空气106送入产品发生器107中，在其中至少部分原料空气被沸腾的液氧所间接热交换冷凝。如果形成的原料空气201中除液体外还包含蒸汽，则可以将物流201通入相分离器108中分成气体和液体。气体111用部分通过热交换器112的方法冷凝后通入塔105中作为物流720的一部分。液体或被冷凝的原料空气109在热交换器110中与液体氧间接热交换后进一步冷却，并将形成的物流699与物流720合并通入塔105之中。
塔105是双塔深冷空气分离设备的高压塔，通常在60-90磅/平方英寸绝压(psia)压力下运行。在塔105中，进入其中的原料被深冷精馏分离成富氮的气体和富氧的液体。从塔105放出的物流117中的富氧液体，用通过部分热交换器的方法加以进一步冷却，然后通入氩塔132的顶部冷凝器131中，在其中被冷凝的粗氩蒸气部分汽化。将从顶部冷凝器131放出的气体和残留的液体分别作为物流202和203送入塔130之中。将来自塔105的富氮气体作为物流204送入主冷凝器205中，在其中与再沸塔130底部物料进行间接热交换被冷凝。将形成的富氮液体206至少分成两股物流118和207，将物流207返送入塔105中作为回流，而将物流118通过部分热交换器112进行冷却后送入塔130中。
将来自塔130的物流134(主要含氧和氩)送入氩塔132中，在其中用深冷精馏法分离成粗氩气体和富氧液体，后者作为物流133被返送入塔130之中。粗氩气体中氩浓度一般至少达95％，在顶部冷凝器131中用富氧液体按上述方式冷凝。将形成的液体粗氩中一部分208返送到塔132中作为回流，同时将另一部分粗氩121通入热交换器122中按上述方式汽化，并加以回收作为粗氩209。
塔130是双塔空气分离设备的低压塔，其操作压力比塔105低，一般处于17-30psia范围内。送入塔130中的各种原料在该塔中被深冷精馏分离成富氮液体和富氧液体。富氮气体从塔130中以物流114放出后，通过热交换器112和101使之加热，然后可以回收作为气体氮产品流210。此氮产品气的纯度一般至少为99.99％。必要时可以从塔130中放出富氮液流119作为液氮产品。为了保证产品纯度，在比塔130中放出物流114的位置低的某处，从塔130中放出废气流115，而使之通过热交换器112和101加热后以物流211的形式从***中排出。
富氧液体氧纯度一般至少为99.5％，将其从塔130中以物流212放出，必要时使之通过泵140加压到较高压力。如果深冷精馏***不含氩塔，则富氧液体可能有较低的最低氧纯度，例如90或95％。然后使被加压的液体氧流213作为体流141通过热交换器110，接着送入产品发生器17之中，使之在其中汽化以便对原料空气进行冷凝。形成的氧流143经过热交换器101加热后，回收作为气体氧产品流620。当直接将产品气体氧送到使用地点时，回收所说的气体氧包括将气流620直接送到使用地点，例如炼钢厂。
在气体氧产品的需求量小于液体氧的生产速度期间内，并不降低深冷空气分离设备的运行速度，可以在该设计的速度下使该设备连续生产产品并且可以将过量的液态氧通过物流116送入液氧贮罐650中用于产生备用的液氧。当气体氧产品的需求量超过液氧的生产速度时，可以利用阀门600将贮罐650中的备用液体氧送入物流141中，用这种方法增加液氧向产品发生器107流动的流量。为了平衡产品发生器107中的热交换，随着液氧流量的增加相应增大输入产品发生器107中的原料空气流量，结果导致生产出过量冷凝空气。
本发明将液态空气贮罐和产品发生器结合起来。通过采用产品发生器汽化液态氧，就不必将大量热能供入***之中。由汽化液态氧回收得到的冷量被返送到深冷精馏设备中。按本发明产生过量液态空气的情况下，将冷凝的过量原料空气经物流700送入液态空气贮罐750之中，以便生产备用液态空气；当需要保持深冷精馏设备的设计操作速率时，将备用的液态空气经由物流710和720送入塔105之中。虽然附图中说明的贮罐650和750是单个贮罐，但是应当想到这两种贮罐之一或二者都可以是贮罐组。
本发明的一个重要内容是液态空气贮罐750。用管路将过冷的液态空气流699送入液态空气贮罐750和塔105之中。调节物流700和710的流量，来维持向塔105送入所需的液态空气720的用量。在稳态下，液氧的附加流量600和液态空气700向贮罐750的流量应当是零。气态氧需要量增加时，增加物流100、106、143、600和700的流量来满足要求，同时其它设备的流量可以基本上维持不变。当气体氧需要量减少后，将物流100、106和143的流量减小到稍低于其稳态值的数值下，并且将物流600和700减少到零。向产品发生器107中输入的空气流106减小时，将降低从热交换器器110中放出的液态空气流710流量。首先从贮罐750放出液态空气流710以维持向塔105流入恒定量液态空气720。增加流入贮罐650的液氧流116流量以维持恒定的塔条件。
氧流143的压力，取决于空气流106的压力和流量、产品发生器107的设计和物流141的压力。可以使用液体泵和/或专用罐来将物流141的压力提高到所需的水平。液氧产品可以直接送入贮罐650，或从产品发生器107中放出，经热交换器112过冷之后由管道送到外部贮罐之中。
控制气体氧物流143压力的能力，是本发明的关键性优点，尤其是使用产品氧压缩机时更是如此。通过在产品发生器中汽化液态氧同时使高压原料空气冷凝的方式生产高压氧气。通常的空气分离设备生产氧产品气体的压力，由塔操作压力决定。为了提高产品气压力，必须在效率显著损失的条件下提高整个塔***的压力。本发明能够使额外的空气压缩机作业转变成骤冷器102中的致冷作用，无需提高塔***中的压力。这样一来，提高了塔***中的净液体生产量和消除了其中的物理限制，例如塔130中的压力额定值。
液体氧贮罐750由于可以在无需强化塔操作的条件下通过从贮罐650额外送料来提高气体氧产品的产量而进一步改善所说的过程。由于在气体氧的瞬时产量、平均产量和致冷作用之间不再互相联系而扩大了所说***的操作范围。液态空气贮存可以使诸参数的以独立地控制。液态空气贮罐还更容易减少氧产品的排放，因为在有过量氧分子存在下可以获得一种现成的致冷源。而具有贮罐的普通***在贮罐装满时会要求排放掉过量的氧分子。
在高需求量期间为了提高设备的能力，优选提高氧产品压缩机的进料压力，而不采用从贮罐中汽化液体增压法。在低需求量期间，可以减小氧压缩机的吸气压力来尽可能地减小能耗。在普通的空气分离设备中，用减压阀来降低氧产品物流的压力。本发明的效率更高，因为它可以使物流100中的原料空气压力得到降低作为所需的氧压力降。原料空气压力的下降低减小了能耗。
本发明的另一种有益应用的情况是能量成本逐日有很大差别的场合。此时，可以用空气提供产品发生器107中的气体驱动力，并把液化的全部空气送入贮罐750之中。在能量成本高的时期，送入产品发生器107中的氧原料142可以全部或大部分来自贮罐650。而当能量成本低的时期，可以增大空气流量，并把蒸馏塔投入运行。来自贮罐750的液态空气可以作为分子和致冷作用源供给塔130。在低能量成本时期的氧总产量，会显著地高于平均需要量。当蒸馏塔105和130未运行时，就会在物流116中产生足够量液氧产品供给热交换器107。
虽然本发明是参照某个优选方案加以详细说明的，但是本领域中普通技术人员会想到在权利要求的实质和范围内有本发明的其它一些方案。

Claims (6)

1．一种通过深冷精馏原料空气来生产气体氧的方法，包括：
(A)将原料空气通入产品发生器中，与所说产品发生器中的液态氧进行间接热交换后冷凝进料空气；
(B)将冷凝的原料空气通入包括高压塔和低压塔的深冷精馏设备中，以生产液态氧；
(C)将在深冷精馏设备中生产的液态氧送入产品发生器中，以便对原料空气进行冷凝，并从产品发生器中回收气体氧产品；
(D)泵送在深冷精馏设备中生产的液态氧后将泵送的液态氧送入液氧贮罐，以生产储备的液态氧；
(E)利用从液氧贮罐向产品发生器中通入液氧，增大向产品发生器输送液氧的流量，同时相应增大原料空气向产品发生器中的流量，以生产过量冷凝的原料空气；
(F)将产品发生器中生产的过量冷凝的原料空气送入液态空气贮罐，同时不经过液态空气贮罐而连续将冷凝的原料空气通入深冷精馏设备中；以及
(G)将另一部分原料空气膨胀并将该部分膨胀的原料空气送入高压塔。
2．根据权利要求1的方法，其中还包括将来自深冷精馏设备中的含氩流体送入氩塔，并从所说的氩塔回收氩浓度至少为95％的氩流体。
3．一种生产气体氧的深冷空气分离设备，包括：
(A)产品发生器、向产品发生器供给原料空气的装置和从产品发生器向包括高压塔和低压塔的深冷精馏设备输送液体的装置；
(B)从深冷精馏设备向产品发生器输送液体的装置和从产品发生器回收气体产品的装置；
(C)液氧贮罐、泵、从深冷精馏设备向泵输送液体的装置和从泵向液氧贮罐输送液体的装置，以及从液氧贮罐向产品发生器输送液体的装置；
(D)液体空气贮罐、从产品发生器向液体空气贮罐输送液体的装置和从液体空气贮罐向深冷精馏设备输送液体的装置并且其中在(A)中所述的从产品发生器向深冷精馏设备输送液体的装置不包括液体空气贮罐；以及
(E)膨胀器、向膨胀器供给原料空气的装置和从膨胀器向高压塔输送原料空气的装置。
4．根据权利要求3的深冷空气分离设备，其中还包括氩塔、将来自深冷精馏设备的流体送入氩塔的装置和从所说氩塔回收流体的装置。
5．根据权利要求1的方法，其中还包括通过与液态氧间接热交换而将冷凝的原料空气冷却，然后再将该冷凝的原料空气通入深冷精馏设备。
6．根据权利要求3的深冷空气分离设备，其中还包括热交换器，从产品发生器向热交换器输送液体的装置和从热交换器向深冷精馏设备输送液体的装置。
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EP0556861B1 (en) 1996-09-25
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US5265429A (en) 1993-11-30
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JPH0611253A (ja) 1994-01-21
BR9300619A (pt) 1993-08-24
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MX9300929A (es) 1993-08-01

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