CN108286870A - 一种低温精馏制取液体的方法 - Google Patents

一种低温精馏制取液体的方法 Download PDF

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CN108286870A
CN108286870A CN201810156290.7A CN201810156290A CN108286870A CN 108286870 A CN108286870 A CN 108286870A CN 201810156290 A CN201810156290 A CN 201810156290A CN 108286870 A CN108286870 A CN 108286870A
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air
rectifying
tower
liquid
nitrogen
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孙世学
储波
阮家林
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Zhejiang Fortune Cryogenic Equipment Co Ltd
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Zhejiang Fortune Cryogenic Equipment Co Ltd
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Abstract

本发明涉及一种低温精馏制取液体的方法。一种低温精馏制取液体的方法，包括如下步骤：步骤1：原料空气经过空气压缩机、空气预冷系统和空气纯化系统；步骤2：纯化后的空气连续进入换热器，换热器内的空气分为两股；第一股空气经过换热器冷凝成液空进入精馏下塔；第二股空气抽出后进入低温膨胀机进行膨胀，部分空气进入精馏下塔，另一部分空气返回换热器复热膨胀后返回空气压缩机进口或空气预冷系统中；步骤3：节流进下塔的液空和膨胀后的部分空气进入精馏下塔进行精馏，得到液氮产品；而后经精馏上塔进一步精馏得到液氧产品。该方法有效降低循环空压机的排压，提高膨胀机单位制冷量，从而达到使设备易于操作、减小设备初步投资的目的。

Description

一种低温精馏制取液体的方法
技术领域
本发明涉及一种低温精馏制取液体的方法。
背景技术
目前液体空分产品需求量仍然越大，但液体量较大且品种要求较多时，空分系统所涉及的动设备的数量及工作压力就比较高。常规制取大量液体产品的流程：原料气空压机经过三级压缩增压到0.62MPaA后进入预冷和纯化系统除去杂质，经纯化后的空气除部分作为空分装置自用仪表气外，其余全部进入循环空压机增压。增压后的空气经末冷后抽出一部分进高压主换冷却后去高温膨胀机膨胀，复热返回循环增压机入口处，其余全部进高温膨胀机和低温膨胀机的增压端进行连续增加，二次增压后的空气经增压端冷却器冷却后进高压主换冷却，部分经高压主换冷却到一定的温度去低温膨胀机膨胀并部分返回到循环空压机的入口，其余继续冷却为全液体节流进下塔。由于循环空压机入口压力是纯化后的空气压力即比低压空压机的排压稍低，为了使装置达到冷量平衡，高低温膨胀机膨胀端的进气压力就比较高。致使循环空压机、高低温膨胀机、高压板式的实际工作压力就很高，且空气增压到所需压力一般需要低压空压机和循环空压机共同完成。这种情况一方面无形中增加了设备的投资成本，增大占地面积,另一重要缺憾是设备的工作压力较高，不易操作。因此从装置的经济性的角度考虑，液体空分流程还有较大的改进空间。
发明内容
为了解决上述问题，本发明的目的在于提供一种低温精馏制取液体的方法，该方法有效降低循环空压机的排压，从而降低高低温膨胀机、高压板式的工作压力，提高膨胀机单位制冷量，从而达到使设备易于操作、减小设备初步投资的目的。
为了实现上述的目的，本发明采用了以下的技术方案：
一种低温精馏制取液体的方法，其特征在于：包括如下步骤：
步骤1：原料空气经过空气过滤器去除灰尘和机械杂质，进入原料空气压缩机增压，再经过空气预冷系统降温，然后进入空气纯化系统用以去除原料空气中的H2O、CO2、C2H2等不纯物质；
步骤2：纯化后的空气连续进入高温膨胀机和低温膨胀机的增压端增压，经过增压端冷却器冷却后进入换热器，换热器内的空气分为两股；第一股空气经过换热器冷凝成液空，引出后经过节流直接进入精馏下塔进行精馏；第二股空气由换热器合适位置抽出进入低温膨胀机进行膨胀，第二股空气膨胀后部分空气进入精馏下塔进行精馏，另一部分空气返回换热器复热到一定温度后进入高温膨胀机膨胀到常压复热，而后返回空气压缩机进口或空气预冷系统中；
步骤3：节流进下塔的液空和膨胀后的部分空气进入精馏下塔进行精馏，在精馏下塔顶部得到纯氮气，并经过冷凝蒸发器液化成液氮，经过过冷器过冷后部分抽出作为液氮产品；精馏下塔得到的液空、纯液氮和污液氮经过冷器后节流进入精馏上塔；经精馏上塔进一步精馏后，在上塔底部获得液氧，液氧引入冷凝蒸发器后，从主冷凝蒸发器的外侧抽出液氧，并经过过冷器过冷后抽出作为液氧产品。
作为优选，所述步骤3中还包括将精馏上塔的液氧经过循环液氧泵输送至冷凝蒸发器，在冷凝蒸发器内的液氧与精馏下塔内上升的氮气换热，氮气被冷凝为液氮返回精馏下塔作为回流液维持精馏，液氧蒸发后的氧气返回精馏上塔作为上升气维持精馏。
作为优选，还包括步骤4；从精馏上塔引出污氮气经过冷器和换热器复热引出后分成两股；一股氮气进入空气纯化系统的加热器，加热器与分子筛吸附器之间构成回路，该股污氮气作为分子筛再生气体；另一股污氮气进入水冷却塔，水冷却塔与空气冷却塔之间构成回路，该股污氮气利用其自身的干燥吸湿特性降低循环水的温度。
本发明采用上述技术方案，该技术涉及一种低温精馏制取液体的方法，该方法中空气经压缩机压缩后，先进入空气预冷系统冷却，然后进入空气纯化系统脱除水分和二氧化碳，纯化后的空气进入高低温膨胀机增压端增压后再进入冷箱。冷箱内包含：高压主换热器、过冷器，精馏塔、主冷凝蒸发器、高低温膨胀机。空气经空压机压缩，全部经预冷和纯化系统后进高温膨胀机和低温膨胀机的增压端。经增加端冷却后进高压主换，部分从高压主换抽出去低温膨胀机膨胀，膨胀后的部分空气进下塔作为下塔的上升蒸汽，其余部分返回高压主换复热到一定温度进入高温膨胀机膨胀，膨胀后的气体复热返回空压机的入口。由于高温膨胀机膨胀后的压力是常压，从而提高了膨胀机的单位制冷量，因此空压机、高低温膨胀机、高压主换的工作压力明显降低。从而达到了降低设备投资、使设备易于操作的目的。
附图说明
图1为本发明的结构示意图。
具体实施方式
下面结合附图，对本发明的优选实施方案作进一步详细的说明。
实施例1
如图1所示的一种低温精馏制取液体的装置，包括过滤器1、空压机2、预冷系统、纯化系统和冷箱。冷箱包括箱体，以及处于箱体内部的换热器3和精馏系统，以及连接在箱体外侧的低温膨胀机4和高温膨胀机5。所述过滤器1、空压机2、预冷系统和纯化系统依次连接，纯化系统引出的管路依次经过高温膨胀机5和低温膨胀机4后引入换热器3中，换热器3内的管路分为两路，第一管路a由换热器3末端引出后引入精馏系统中。第二管路b由换热器3中部引出经过低温膨胀机4后分为第一支路c和第二支路d，第一支路c直接引入精馏系统中，精馏系统末端引出液氧输出管路e和液氮输出管路f。第二支路d返程引入换热器3复热，又由换热器3引出后经过高温膨胀机5再次引入换热器3复热，最终由换热器3引入到空压机2进口或预冷系统中。所述第二支路与第一管路a在换热器3内进行热交换。
具体地，所述精馏系统包括冷凝蒸发器6、过冷器7、精馏上塔8和精馏下塔9。第一管路a由换热器3末端引出后引入精馏下塔9，精馏下塔9的塔顶区域通过冷凝蒸发器6冷凝形成液氮，液氮输出管路f在较高压力的作用下，由精馏下塔9的塔顶区域引出后后经过冷器7向外输出。所述精馏下塔9通过管路依次连接过冷器7和精馏上塔8，精馏上塔8通过管路与冷凝蒸发器6构成回路，冷凝蒸发器6与精馏下塔9的塔顶区域进行热交换。所述液氧输出管路e在压力作用下，由冷凝蒸发器6引出后经过冷器7向外输出。
所述空气纯化系统包括加热器11和两组交替使用的分子筛吸附器10，两组分子筛吸附器10并联设置，加热器11与分子筛吸附器10之间构成回路。所述预冷系统包括空气冷却塔12和水冷却塔13，水冷却塔13与空气冷却塔12之间构成回路。所述精馏上塔8的塔顶引出污氮气管路g，经过过冷器7和换热器3后分别连接空气纯化系统和预冷系统。具体是，污氮气管路g连接在空气纯化系统的加热器11和预冷系统的水冷却塔13上。该技术方案中，所采用的空冷塔与分子筛吸附器10由于提高了操作压力，减小了加工空气的体积流量，容器的外形尺寸相应减小，从而减小设备的占地面积，节省部分压力容器的投资成本。另外由于容积设备外形尺寸的减小，可以避免出现运输尺寸超限的问题。
上述技术方案涉及一种低温精馏制取液体的装置，该低温精馏制取液体的装置使用时，纯化后的空气进高低温膨胀机5、4连续的增压，提高液化空气的压力，使液化更易进行。低温膨胀机4膨胀后的部分空气作下塔的上升气，使下塔的精馏工况持续进行，同时部分低温膨胀机4膨胀后的空气返回主换3复热到一定的温度并进入高温膨胀机5去膨胀到常压，一方面提高了冷量的品质另一方面增大了膨胀比，使单位制冷效果更佳。从而大大降低循环压缩机的排压，使整个空分系统运行的压力降低。此外，膨胀后的空气返回空压机2，减少外部杂质对空压机2叶轮的影响，同时干燥洁净的空气也减少了纯化系统的负荷，对延长整套空分的运行寿命有明显的提高。或者膨胀后的空气去水冷塔来降低冷冻水的温度。
实施例2：
本实施例是基于实施例1中低温精馏制取液体的装置，所采用的低温精馏制取液体的方法，其包括如下步骤：
步骤1：原料空气经过空气过滤器去除灰尘和机械杂质，进入原料空气压缩机增压，再经过空气预冷系统降温，然后进入空气纯化系统用以去除原料空气中的H2O、CO2、C2H2等不纯物质。
步骤2：纯化后的空气连续进入高温膨胀机和低温膨胀机的增压端增压，经过增压端冷却器冷却后进入换热器，换热器内的空气分为两股；第一股空气经过换热器冷凝成液空，引出后经过节流直接进入精馏下塔进行精馏；第二股空气由换热器合适位置抽出进入低温膨胀机进行膨胀，第二股空气膨胀后部分空气进入精馏下塔进行精馏，另一部分空气返回换热器复热到一定温度后进入高温膨胀机膨胀到常压复热，而后返回空气压缩机进口或空气预冷系统中。
步骤3：节流进下塔的液空和膨胀后的部分空气进入精馏下塔进行精馏，在精馏下塔顶部得到纯氮气，并经过冷凝蒸发器液化成液氮，经过过冷器过冷后部分抽出作为液氮产品；精馏下塔得到的液空、纯液氮和污液氮经过冷器后节流进入精馏上塔；经精馏上塔进一步精馏后，在上塔底部获得液氧，液氧引入冷凝蒸发器后，从主冷凝蒸发器的外侧抽出液氧，并经过过冷器过冷后抽出作为液氧产品。此外在冷凝蒸发器内的液氧与精馏下塔内上升的氮气换热，氮气被冷凝为液氮返回精馏下塔作为回流液维持精馏，液氧蒸发后的氧气返回精馏上塔作为上升气维持精馏。
步骤4；从精馏上塔引出污氮气经过冷器和换热器复热引出后分成两股；一股污氮气进入空气纯化系统的加热器，加热器与分子筛吸附器之间构成回路，该股污氮气作为分子筛再生气体；另一股污氮气进入水冷却塔，水冷却塔与空气冷却塔之间构成回路，该股污氮气利用其自身的干燥吸湿特性降低循环水的温度。
上述技术方案涉及一种低温精馏制取液体的方法，该方法中空气经压缩机压缩后，先进入空气预冷系统冷却，然后进入空气纯化系统脱除水分和二氧化碳，纯化后的空气进入高低温膨胀机增压端增压后再进入冷箱。冷箱内包含：高压主换热器、过冷器，精馏塔、主冷凝蒸发器、高低温膨胀机。空气经空压机压缩，全部经预冷和纯化系统后进高温膨胀机和低温膨胀机的增压端。经增加端冷却后进高压主换，部分从高压主换抽出去低温膨胀机膨胀，膨胀后的部分空气进下塔作为下塔的上升蒸汽，其余部分返回高压主换复热到一定温度进入高温膨胀机膨胀，膨胀后的气体复热返回空压机的入口。由于高温膨胀机膨胀后的压力是常压，从而提高了膨胀机的单位制冷量，因此空压机、高低温膨胀机、高压主换的工作压力明显降低。从而达到了降低设备投资、使设备易于操作的目的。

Claims (3)

1.一种低温精馏制取液体的方法，其特征在于：包括如下步骤：
步骤1：原料空气经过空气过滤器去除灰尘和机械杂质，进入原料空气压缩机增压，再经过空气预冷系统降温，然后进入空气纯化系统用以去除原料空气中的H2O、CO2、C2H2等不纯物质；
步骤2：纯化后的空气连续进入高温膨胀机和低温膨胀机的增压端增压，经过增压端冷却器冷却后进入换热器，换热器内的空气分为两股；第一股空气经过换热器冷凝成液空，引出后经过节流直接进入精馏下塔进行精馏；第二股空气由换热器合适位置抽出进入低温膨胀机进行膨胀，第二股空气膨胀后部分空气进入精馏下塔进行精馏，另一部分空气返回换热器复热到一定温度后进入高温膨胀机膨胀到常压复热，而后返回空气压缩机进口或空气预冷系统中；
步骤3：节流进下塔的液空和膨胀后的部分空气进入精馏下塔进行精馏，在精馏下塔顶部得到纯氮气，并经过冷凝蒸发器液化成液氮，经过过冷器过冷后部分抽出作为液氮产品；精馏下塔得到的液空、纯液氮和污液氮经过冷器后节流进入精馏上塔；经精馏上塔进一步精馏后，在上塔底部获得液氧，从主冷凝蒸发器的外侧抽出液氧，并经过过冷器过冷后抽出作为液氧产品。
2.根据权利要求1所述的一种低温精馏制取液体的方法，其特征在于：所述步骤3中还包括在冷凝蒸发器内的液氧与精馏下塔内上升的氮气换热，氮气被冷凝为液氮返回精馏下塔作为回流液维持精馏，液氧蒸发后的氧气返回精馏上塔作为上升气维持精馏。
3.根据权利要求1所述的一种低温精馏制取液体的方法，其特征在于：还包括步骤4；从精馏上塔引出污氮气经过冷器和换热器复热引出后分成两股；一股氮气进入空气纯化系统的加热器，加热器与分子筛吸附器之间构成回路，该股污氮气作为分子筛再生气体；另一股污氮气进入水冷却塔，水冷却塔与空气冷却塔之间构成回路，该股污氮气利用其自身的干燥吸湿特性降低循环水的温度。
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