CN1074462C - 向氧气炼钢和炼铁过程供氧的方法和设备 - Google Patents

向氧气炼钢和炼铁过程供氧的方法和设备 Download PDF

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CN1074462C
CN1074462C CN97113017A CN97113017A CN1074462C CN 1074462 C CN1074462 C CN 1074462C CN 97113017 A CN97113017 A CN 97113017A CN 97113017 A CN97113017 A CN 97113017A CN 1074462 C CN1074462 C CN 1074462C
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oxygen
tower
rectifying
volume
steelmaking
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CN1171445A (zh
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S·R·克拉尔
M·I·迈尔
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BOC Group Ltd
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Abstract

一种向氧气炼钢过程和炼铁过程供氧的方法，它包括通过空气的精馏使氧与空气分离，将自精馏的第一氧流供往炼钢过程，将自精馏的第二氧流供往炼钢过程，其中第一和第二氧流基本上都自精馏的相同的级排出，且都含97-98%(体积)的氧和小于100ppm(体积)的氮。

Description

向氧气炼钢和炼铁过程供氧的方法和设备
本发明涉及向氧气炼钢和炼铁过程供氧的方法。
氧气炼钢是现代工业经济的主要构成部分之一。现有不同的氧气炼钢工艺的门类，这包括平炉法、底吹炼钢法(包括Bessemer和Q-BOP法)、顶吹转炉法(包括LD-AC法(还有称为BOS(碱性氧气炼钢)或BOP(碱性氧气法)的已知方法)，及包括向铁水吹氧步骤的电弧炉法。
因为氮对钢有有害的影响，所以在这些氧气炼钢法中总是使用高纯度(即氧纯度大于99％)的氧。为产生这种高纯度的氧，通过精馏将空气分离。空气的组成是这样的：为了达到这样的纯度水平，从中取得氧产物的精馏塔具有将氩与氧分离的部分。由于氩和氧有彼此相似的挥发性，所以该部分实质上成为精馏塔的总高度的原因之一，和空气分离法的总能量需要的原因之一。
现代空气分离工艺的一般目标是：不过分增加投资成本而将分离空气厂的能耗降至最小。
有时要求同一空气分离厂供应炼钢和炼铁过程。炼铁过程可采用常规的高炉，高炉所装的炉料包括氧化铁、焦炭和至少一种造渣剂或熔剂，或是所谓的直接还原法，其中用煤代替焦炭。按直接还原法，将炉料装到还原容器中，铁矿石在其中被含氢或一氧化碳的气体混合物还原，而所得的铁在第二容器中熔化，同时煤在其中同时气化，以使产生还原气体混合物。95％纯氧一般被用作煤的气化。结果当还要求氧产物的纯度大于99％时，空气分离厂的投资和运行成本较小。但是，一旦要求生产这样纯的氧产品时，就需要使高纯度的液氧在自取得该氧产物的精馏塔的底部再沸腾。氧的纯度越高，其在给定的压力下的再沸腾温度越高。结果，用于使高纯度氧再沸腾的压力随着氧纯度的升高而升高，因此在使这种气体压力升高方面要作更多的工作。进而，当要求不同纯度的氧产品时，就增加与附加管路和分配器相关的费用。
本发明从事于这些问题。
按照本发明的第一个目标，提供一种氧气炼钢方法，它包括使铁水与通过精馏从空气中分离出来的氧气流接触的步骤，其中氧气含97-98％(体积)的氧且小于100ppm(体积)的氮。
按照本发明的第二个目标，提供一种向氧气炼钢和炼铁过程供氧的方法，它包括通过空气的精馏使氧与空气分离，将精馏的第一氧流供往炼钢过程，将精馏的第二氧流供往炼铁过程，其中第一和第二氧流基本上都自精馏的同一级排出，并都含97-98％体积的氧和小于100ppm体积的氮。
按照本发明的第三个目标，提供一种设备，它包括炼钢容器，炼铁容器及用于使氧与空气分离的精馏塔，其中该炼铁容器和炼钢容器与该精馏塔的同一级是连通的，该级在塔中的位置要使得炼铁容器和炼钢容器在使用时得到含97-98％(体积)的氧和小于100ppm(体积)的氮的氧产品。
通过取得作为产品的含97-98％(体积)氧气，与可比的其中产生纯氧产物的精馏塔相比，在自其取得氧产物的该精馏塔中基本上需要很少的级。进而，按用本发明的方法和设备，该精馏塔的再沸腾可在较低的压力下通过与气流的间接热交换而完成，该压力低于其中产生纯氧产物的可比的精馏塔中的压力，从而可能节能。通过全部采用97-98％(体积)纯度的氧，而不采用纯度95％的第一氧产物和纯度99.7％(体积)的第二氧产物确实达到了空气分离的运行成本和资金值的下降。
较好的是，氧中的氮含量小于50ppm(体积)，而更好是小于10ppm(体积)。即使氧纯度在97-98％(体积)的范围内也可容易地达到这样低的氮杂质的水平，特别是，如果自其取得氧的精馏塔是一个运行上与较高压精馏塔联结的低压塔，而且如果自该低压塔中排出富氩的氧气流以便在另一精馏塔中分离尤为如此。由于排出了富氩氧气流，有效地从低压精馏塔中的氧-氩分离级中排出氮杂质。现已发现，在该氧气流中的氮杂质的含量可通过控制流经与另一塔的头联结的冷凝器的冷却剂的流量而有效地控制。
供给炼钢过程的氧产物就是供给炼铁过程的氧产物，最好是取自精馏塔的底部区(即在该塔中的所有的液体-蒸气接触件以下的区域)。该氧流可以液态，或以蒸气态，或一种为液态而其它为蒸气态取得。
一般来说，将10-30％的总的氧气产物供往炼钢过程，其余的供往炼铁过程。
本文所用的术语“精馏塔”指的是冷凝或分馏塔、区，其中液相和蒸汽相逆流接触，比如，通过使蒸气相和液相在安装于塔、区中的填料件或一系列垂直隔开的盘或板上接触，从而完成流体混合物的分离或提纯。在分离容器中的精馏塔可包含多个分馏区，从而避免了单个容器过份地高。比如，已知在氩精馏塔中采用高度相当于200块理论上的板填料。若将所有这些填料装在单个容器中，则该容器的高度一般会超过50m。因此，按两个分离容器来建造氩精馏塔，从而避免必须采用单个过高的容器是明显合乎要求的。
现将通过实施例，参阅作为空气分离厂的示意性流程图的附图说明本发明的方法和设备，分离厂将高压第一氧流供往炼钢过程，将高压第二氧流供往炼铁过程。
该附图没有标尺寸。
参阅附图，空气流在压缩机2中被压缩。在后冷却器4中散去压缩空气的压缩热。所得的供入的压缩空气流从后冷却器4经能有效地自其中去除水蒸汽和二氧化碳的提纯装置6流出。装置6采用了进行去除水蒸气和二氧化碳的吸附剂床(未示出)。这种提纯装置及其运行在本技术领域中是已知的，所以本文中无需再作说明。
部分提纯的空气流经主热交换器8从其暖端10流向其冷端12，借此将其从大约室温冷却到大致其饱和温度。这样冷却过的空气流在蒸气态下经入口16进入高压精馏塔14的底部区。高压精馏塔14的运行压力在其顶部一般约为0.5兆帕(5巴)的绝对压力。
另一部分提纯的空气流取自主热交换器8的上游，再于增压压缩机18中进一步压缩。在后冷却器20中从该进一步压缩的空气中散去压缩热。此空气流从后冷却器20经主热交换器8从其暖端10流向其冷端12。借此使该空气流流化。所得的液态空气流借助于节流阀22经入口23在高于入口16的水平面流入高压精馏塔14。
该高压精馏塔14包含液体-蒸汽接触装置(未示出)，如网状盘或填料件以便进行上升的蒸汽与下降的液体之间的密切接触。借此将空气分离成位于塔14底部的富氧液态空气馏份和位于塔14顶部的氮蒸汽馏份。氮蒸汽流从塔14的顶部流入再沸腾冷凝器24，并通过与沸腾的液体的间接热交换冷凝。第一部分所得的氮冷凝物被返回到高压精馏塔14，从而为塔提供了回流。通过泵26将第二部分氮冷凝物加压至选定的高压，再经主热交换器8从其冷端12流向其暖端10，然后通过与空气流的间接热交换在其中蒸发。结果形成加压的气体氮产物。得自再沸腾冷凝器24的第三部分氮冷凝物在热交换器28中再冷却，流经节流阀29，再经入口32被引入低压精馏塔30的顶部区。低压塔30以其顶部小于0.15兆帕(1.5巴)的绝对压力运行。
将一般含30-40％(体积)氧的富氧液态空气流从高压精馏塔14经出口34排出，再以与该氮冷凝物相同的大概方向经热交换器28流动。结果该富氧液态空气被再冷却。所得的再冷却的富氧空气被分成两个流。一个流直接通过节流阀36，再经入口43流入低压精馏塔30。另一流再冷却的富氧液态空气通过与氩塔40相联的冷凝器38。由于其在与冷凝氩相联系的冷凝器38中的热交换，该富氧液体在冷凝器38中蒸发。所得的蒸汽也流向低压精馏塔30，它是经入口42被引入该塔的。
此外，通过从主热交换器8中的中部区域以大致高压精馏塔14的压力取一个提纯空气的流，和在一台膨胀涡轮机46中进行附加的作业使其膨胀形成为在低压精馏塔30中分离的空气。该膨胀的空气在大致其饱和的温度，以使其被引入低压精馏塔30而基本上无任何压降的压力离开涡轮机46。一般将此膨胀的空气流与取自冷凝器38的蒸发的富氧液态空气预混合。
另外，通过经在与入口23相同水平面的出口39从高压精馏塔排出液态空气流可提供为在低压精馏塔中分离的空气。该液态空气流通过流经热交换器28被再冷却，然后流经节流阀41再经入口44被引入低压精馏塔30。一般来说，经入口44引入塔30的液态空气的流量为经入口23被引入高压精馏塔14的液空气流量的2/3-3/4。
低压精馏塔30包含填料件48(一般是装配的填料)，它能使上升的蒸汽与下降的液体接触。这种接触的结果，发生空气的分离。液态氧馏份被收集于低压精馏塔30的低部而氮蒸气馏份被收集于低压精馏塔30的顶部。经塔30向上的蒸汽流通过部分液氧馏份在再沸腾器一冷凝器24中通过与冷凝的氮蒸汽间接热交换来蒸发而产生。将富氩氧蒸汽流经出口50从低压精馏塔30的中部水平面排出，然后流到另一个精馏塔40，而且它具有从塔40中分离出来的氩。氩塔40被分成两部分。有第一部分-氩精馏塔52和第二部分-氩精馏塔54。塔52部分和54部分都包含填料件56，比如装配的填料，以使在其中进行密切的液体-蒸汽接触。在塔52部分的底部区域接受富氩氧蒸汽流，塔54部分的顶部在运行上与氩冷凝器38相联系。液态氩流从冷凝器38向下经塔54部分流出，通过泵58自其底部将它输往塔52部分的顶部。该液体在塔52部分中与富氩氧蒸汽相逆地下降。该蒸汽进一步富集氩，并从塔52部分的顶部流入塔54部分的底部，并于塔54中发生上升的蒸汽与下降的液体之间的进一步接触。结果无氧的氩蒸汽基本上在塔54的顶部产生，且它是流入冷凝器38的蒸汽。随着产物，比如通过从中去除氮而进一步提纯，而从冷凝器38中取得氩冷凝物的流。将于塔52部分底部收集的液体经入口60返回到低压精馏塔30。
氮流经出口62从低压精馏塔30的顶部排出，再通过另一个热交换器26，由此为使其中流再冷却提供必要的冷却。该氮流从热换器26经主热交换器8从其冷端12至其热端10通过，由此被加热到接近室温。经出口64自低压精馏塔30的底部排出液氧流。部分液氧由泵66打到1.0兆帕(10巴)数量级的绝对压力，并从主热交换器8的冷端12向其热端10流过而蒸发。将所得的蒸发的，绝对压力为1.0兆帕(10巴)数量级的氧供到氧气炼钢容器70。用泵72将第二氧气产物流加压至2.0-4.0兆帕(20-40巴)之间数量级的绝对压力，用从泵72经主热交换器8从其冷端12向其暖端10流动，并由此被蒸发。所得的蒸发的氧流以约2.0兆帕(20巴)的绝对压力供往直接还原的Corex炼铁法的气化器74。
低压精馏塔30这样运行：使两级氧产物流含97-98％(体积)的氧，其余基本上是氩。在该氧中不超过10ppm(体积)的氮杂质。此二股氧产物中的其余部分由氩和痕量的杂质，如氙、氪和甲烷组成。在氧产物中的氮杂质的含量可借助位于向冷凝器38供富氧液态空气的管道中的流量控制阀80间接地控制。经过冷凝器38的富氧液态空气的流速越大，首先促使富氩氧蒸气流入精馏塔40的流速越大，其次富氩氧气流中的氮杂质的排出速度越大。氮杂质的排出速度越大，产物氧中的氮杂质含量越低。因此，通过选择阀80的合适地设置，氧产物中的最大氮浓度决不会超出。
在氧产物中存有2-3％(体积)数量级的氩杂质不可避免地伴有氩产物的低回收。但是，即使回收了20％的氩-这里很容易达到的-一般也满足炼铁、炼钢对氩的要求。
本发明的方法不限于任何特定的炼钢或炼铁方法。这些方法的运作可以是常规的。本发明也不限于任何特定的冷冻空气分离方法。比如，可用所谓的“双重再沸腾器”法取代采用单一冷凝器-再沸腾器24的高压精馏塔14和低压精馏塔30的设备。在这种方法中，冷凝器-再沸腾器24与高压精馏塔14隔开，并代之以取自主热交换器8的冷端12下游的和高压精馏塔14的入口16上游的空气流加热。在低压精馏塔30的中部水平面采用第二再沸腾器，以补充再沸腾器24所提供的向上蒸汽流，及使取自高压精馏塔14顶部的氮蒸汽冷凝。这种双重再沸腾器设备的优点在于：一般它们所需的加热压力比附图中所示的那种类型的可比的设备的低。
在附图中所示的工厂的典型的运行实施例中，氧产物的纯度均为97.5％(体积)体积，而且低压精馏塔30包含60％数量级的级数(理论上的盘数)，即它需要采用纯度99.7％的一直被生产的氧产物。一般来说，在此实施例中增压压缩机的绝对出口压力的数量级为2.5兆帕(25巴)。
如果需要，可将少量的，比如1％的经出口64自低压精馏塔30排出的液氧作为液氧产物储存起来，用于其它目的，如切割和火焰清理。不从低压精馏塔30中以液态取得两种主要的氧产物，而可从于再沸器-冷凝器24中形成的，并由主热交换器8下游的压缩机升到高压的蒸汽中取得一种或两种氧产物。
在附图中所说明工艺的基础上，通过以下的对比例说明本发明的优点，其中80％的氧产物的1.1兆帕(11巴)的压力流向Corex炼铁厂，而20％流向碱性氧气(炼钢)厂。
                    常规           本发明炼铁氧产物纯度          95％            97.5％*炼钢氧产物纯度          99.5％          97.5％*氧产物平均纯度          95.9％          97.5％在典型的LP塔30中理论上的盘(级)数        80              50能耗                    100％           98％
*杂质包括2ppm(体积)的氮。
这样，通过本发明就可能将低压精馏塔30的高度大为降低。此外，即使本发明中的氧产物的平均纯度比对比的常规方法中的平均纯度高，仍达到了可观的节能。因为在直接还原炼铁方法中所需的氧一般是氧气炼钢方法所需氧的5-10倍，所以所选的实施例是典型的。
此外，按对比例所得的结果不取决于特定的空气分离方法。的确，如果选用了双重再沸腾器空气分离法，甚至可达到更大的节能。

Claims (8)

1、一种向氧气炼钢和炼铁过程供氧的方法，它包括通过空气的精馏使氧与空气分离，将精馏的第一氧流供往炼钢过程，将精馏的第二氧流供往炼铁过程，其中第一和第二氧流基本上都自精馏的同一级排出，并都含97-98％体积的氧和小于100ppm体积的氮。
2、权利要求1的方法，其中氧取自运行上与高压精馏塔相连系的低压精馏塔。
3、权利要求2的方法，其中从该低压精馏塔排出富氩的氧流为在另一个精馏塔中分离。
4、权利要求3的方法，它还包括控制通过与另一个塔的顶部相关的冷凝器的冷却剂的流量的步骤，以使控制氧中的氮杂质含量。
5、权利要求2的方法，其中氧在低压精馏塔中的全部液体-蒸汽接触件之下取得。
6、权利要求1的方法，其中所述氧中的氮含量小于50ppm体积。
7、权利要求1的方法，其中所述氧中的氮含量小于10ppm体积。
8、用于进行权利要求1所述方法的设备，该设备包括炼钢容器，炼铁容器和用于从空气中分离氧的精馏塔，其中炼铁容器和炼钢容器均与该精馏塔的同一级连通，该级在塔中的位置是这样的：炼铁容器和炼钢容器在使用时均得到含97-98％体积的氧和小于100ppm体积的氮杂质的氧产物。
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EP0805217A3 (en) 1998-05-27
EP0805217B1 (en) 2001-11-28
CN1171445A (zh) 1998-01-28
AU1994297A (en) 1997-11-06
EP0805217A2 (en) 1997-11-05
DE69708500D1 (de) 2002-01-10
DE69708500T2 (de) 2002-07-11
US5980607A (en) 1999-11-09
JPH1072612A (ja) 1998-03-17
GB9609099D0 (en) 1996-07-03
AU729622B2 (en) 2001-02-08

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