CN109764638B - 一种大型制氧机组氩系统变负荷方法 - Google Patents

一种大型制氧机组氩系统变负荷方法 Download PDF

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CN109764638B
CN109764638B CN201811524579.6A CN201811524579A CN109764638B CN 109764638 B CN109764638 B CN 109764638B CN 201811524579 A CN201811524579 A CN 201811524579A CN 109764638 B CN109764638 B CN 109764638B
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argon
valve
tower
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CN109764638A (zh
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赵鹏
贾永忠
宋海波
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Baotou Iron and Steel Group Co Ltd
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
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Abstract

本发明公开了一种大型制氧机组氩系统变负荷方法，通过调节粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的方式使大型制氧机组氩系统达到氩气增产、氩气减产的目的。

Description

一种大型制氧机组氩系统变负荷方法
技术领域
本发明涉及一种大型制氧机组氩系统变负荷方法。
背景技术
包钢动供总厂氧气作业部9#制氧机生产出的氩气产品，除供应公司炼钢用户外，剩余大部分液氩做为液氩产品对外销售，也可以做为后备系统进行贮存。如遇空分装置故障跳车时，通过外置液体泵补充氩气管网压力。但由于外销液氩产品并不稳定，旺季时液氩供不应求，淡季时液氩贮槽全满需向外排放即浪费液氩资源又浪费蒸气还对环境形成噪声污染，造成一定能源浪费。
发明内容
为了解决上述问题，本发明的目的是提供一种大型制氧机组氩系统变负荷方法，达到旺季增产，淡季减产的目的，做到实时调整，减少液氩向外排放消除能源浪费。
为解决上述技术问题，本发明采用如下技术方案，
一种大型制氧机组氩系统变负荷方法，通过调节粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的方式达到大型制氧机组氩系统氩气增产、氩气减产目的；其中Ⅴ701阀位于粗氩Ⅱ塔上部，液空冷凝器进液侧，主要用于控制液空冷凝器中的液空液位，保证液空与粗氩之间的换热效果；
其中氩气增产时具体粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的操作条件如下表：
粗氩流量 1500Nm3/h 1600Nm3/h 1700Nm3/h
V701阀开度 20％一20.5％ 20.3％一20.6％ 20.5％一20.8％
氩馏份氩含量 10～11％Ar 10.5～11.5％Ar 10.5～11.8％Ar
其中氩气减产时具体粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的操作条件如下表：
Figure BDA0001904090470000021
所述Ⅴ701阀开度和氩馏份氩含量根据表中灵活控制，V701开度增大时氩馏份氩含量减小。
进一步的，氩气减产时，Ⅴ3阀开度在0.2-0.5％；Ⅴ3阀位于精馏塔上部，主要用于液氮节流，作为下流液体保证精馏塔上部精准分离。
进一步的，氩气减产时，Ⅴ3阀开度在0.35％。
进一步的，所述V3阀正常工作时开度为66％，膨胀量在23000-24000Nm3/h。
与现有技术相比，本发明的有益技术效果：
通过调节粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的方式使大型制氧机组氩系统达到旺季增产，淡季减产的目的，做到实时调整，减少液氩向外排放消除能源浪费。
附图说明
下面结合附图说明对本发明作进一步说明。
图1为制氩流程示意图。
具体实施方式
如图1所示，制氩流程如下：
(1)此制氧机组流程为制氧外压缩流程，产出介质为氧气、氮气、氩气。主要产出产品为氧气、氮气，但由于近些年炼钢工艺对氩气需求量及纯度要求增高，氩气也成为制氧机组主要产出产品。
(2)图1中左边为制氧机组精馏塔主塔，利用氧、氮、氩三种介质分子间密度不同、沸点不同，下塔初步分离，上塔精馏分离，再通过筛板塔及下流液体(来自主冷凝蒸发器的液氮)层层进行制热交换，精馏分离出高纯的氧气、氮气以及纯度不高的氩馏分(氩气的原料气体)。
(3)从上塔相应部位抽出氩馏分气体约48420m3/h，含氩量为9～10％(体积)，含氮量约0.017％(体积)。氩馏分直接从粗氩Ⅰ塔底部道路，粗氩Ⅰ塔采用粗氩Ⅱ塔底部排除的粗液氩作为回流液，作为回流液的粗液氩经液氩泵AP501(或 AP502)加压后直接进入粗氩Ⅰ塔上部。粗氩自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入。粗氩冷凝器采用过冷后的液空作为冷源，上升气体在粗氩冷凝器中液化，其中一部分未1513m3/h的粗氩气(其组成为99.6％Ar，≤2ppmO2)经V705 阀导入粗氩液化器中进行液化，然后进入纯氩塔中，继续精馏；其余作为回流液入粗氩Ⅱ塔。液空冷凝器蒸发后的液空蒸汽和少量液空同时返回上塔参与精馏(减少能源浪费消耗)。
(4)粗液氩从纯氩塔中部进入，与此同时在纯氩塔精氩蒸发器氮气侧内利用下塔顶部来的压力氮气作为热源，促使纯氩塔底部的液氩蒸发成上升蒸汽，而氮气被冷凝成液氮经节流后进入V3阀(位于精馏塔上部液氮节流阀，主要作为上塔的精馏的下流液体)后，然后返回上塔。来自液氮过冷器并经节流的液氮进入纯氩冷凝器作为冷源，使纯氩塔顶部产生回流液，以保证塔内的精馏，使氩氮分离，从而在纯氩塔底部得到纯液氩。纯液氩可以直接以液态的形式注入用户储槽，也可以在冷箱内经过中压液氩泵加压到3.0MPa(G)汽化回收冷量后送入炼钢用户生产中。
实施例1
本发明提供的一种大型制氧机组氩系统变负荷方法在经过实际操作调节总结出氩系统变负荷操作可采取以下两种有效操作方法:
1)、氩气增产操作法、可将氩气产量从设计值1500Nm3/h增至1700Nm3/h 在氩气供应紧张时补充管网压力，增加液氩产品。
2)、氩气减产操作法、可将氩气产量从1700Nm3/h减至900Nm3/h，以减少液氩产量来达到减少浪费现象达到节能降耗的目的。
但在变负荷过程中又会对主塔和氩系统形成一定的影响。如增、减产过程中会遇到氩系统氮塞，影响到氩气的纯度和生产，也会使主塔氧、氮气纯度下降。在增产过程易使出粗氩Ⅰ塔粗氩气含氧量增加，精氩氧含量升高最终使氩产量下降。所以在变负荷过程中要全盘考虑对主塔和粗氩塔的影响。具体操作方法如下:
一、氩气增产操作法
在操作中要想使氩气产量增加。可采取:
(1)提高氩馏份氩含量、(2)增加上塔抽取的氩馏份量，来提高进入粗氩塔的氩含量，提高氩的提取率以达到增产的目的。但是如果氩馏份氩含量控制过高或者氩馏份量抽取过大又会使带入粗氩塔的氮气量增多造成粗氩塔、精氩塔氮塞。如不采取以上措施而直接提高粗氩量至1700Nm3/h又会使出一塔粗氩氧含量升高，粗氩Ⅱ塔底部液位下降，去粗氩Ⅰ塔的粗液氩量减少，粗氩Ⅰ塔的回流液量减少使岀Ⅰ塔粗氩气氧含量进一步升高，从而形成恶性循环直至粗氩Ⅰ塔不工作，为了保证纯度只能减少氩产量最终达不到增产目的。
所以在操作中可采取逐渐提高粗氩Ⅱ塔液空液位增大粗氩塔冷凝器换热面积来增加冷凝器的热负荷以达到多抽氩馏份的目的。同时控制氩馏份氩含量不要过低或过高。(氩馏份氩含量过低出粗氩Ⅰ塔粗氩含氧升高；氩馏份氩含量过高容易氮塞)。粗氩Ⅱ塔液空液位由于液空纯度变化也会使冷凝器的温差发生变化，根据液空液位来判断也不准确(大约在300mm-340mm之间)在实际操作中主要以Ⅴ701阀的开度来判断氩馏份的抽取量。
具体操作最佳如下表:
粗氩流量 1500Nm3/h 1600Nm3/h 1700Nm3/h
V701阀开度 20％一20.5％ 20.3％一20.6％ 20.5％一20.8％
氩馏份氩含量 10～11％Ar 10.5～11.5％Ar 10.5～11.8％Ar
根据以上表中数据来调节即可以达到氩气增产的目的也可保证工况的稳定运行(如Ⅴ701阀开度大氩馏份氩含量控制可低一些)。
对主塔的影响:由于粗氩产量增加，粗氩液化器和精氩塔所需的冷源液氮量增加，氩系统所需冷量增多，主塔的液氧、液氮的排放量会减少，需适当增加膨胀量来增大制冷量。同时由于液氮的抽取量增多，为了保证液氮纯度可适当关小V3阀(精馏塔上塔液氮节流阀)的开度在(0.2％一0.5％)之间具体可根据液氮纯度来调节。
二、氩气减产操作法
在操作中要想使氩产量减下来，可采取降低粗氩产量；降低粗氩冷凝器的液空液位等手段，来减少冷凝器的热负荷以达到减少氩馏份的抽取量同时减少氩气产量，但采取以上方法各有利敝。
1、当单纯减少粗氩产量时，由于进粗氩塔的氩含量并没有减少，当粗氩气量减少时，粗液氩产量增加，粗氩Ⅱ塔底部液位升高，为了控制粗氩Ⅱ塔底部液位防止过高只能将多余液体打入粗氩Ⅰ塔，造成Ⅰ塔的回流液量过大使主塔氩馏份回流液下部回流比增大液氧纯度下降，富氩区下移氩馏份氩含量升高严重时氮塞。
2、当单纯减少粗氩产量时，由于氩馏份抽取量并没有减少，氩馏份带入的氮量也没有减少，但粗氩由于减产带出粗氩塔冷凝器的氮气量减少而使氮气在冷凝器积聚，当达到一定量时使粗氩塔氮塞影响氩的生产。
3、当降低氩馏份氩含量时，会使主塔富氩区上移，氧产量减少、氧纯度升高，也会使氮的平均纯度下降、氧的提取率下降。同时也会使氩馏份中氧含量升高中，岀一塔的粗氩气含氧量升高影响氩的纯度。
只有将以上三种方法结合使用并调节粗氩量、Ⅴ701阀、氩馏份氩含量、三者之间在最佳位置才能达到即减少粗氩产量又不会影响到主塔和氩系统的工况的稳定运行。
具体操作最佳位置如下表:
Figure BDA0001904090470000061
根据以上表中调节即可达到减产目的也能保证主塔和氩系统工况的稳定运行。Ⅴ701阀开度和氩馏份氩含量要根据表中灵活控制，V701开度大，氩馏份氩含量可控制低一些。
对主塔的影响:由于粗氩产量减少，氩馏份的抽取量减少，使上塔的上升气量增大，回流比减小富氩区上移，氧纯度升高、氮纯度下降，氩系统消耗的冷量也减少。此时可适当开大Ⅴ3阀在0.2-0.5％之间保证气氮纯度具体可根据气氮和液氮纯度来调节(V3阀正常时大约在66％左右，膨胀量在23000-24000Nm3/h，但随着进下塔空气含湿量的变化V3阀的开度也有所变化)。同时由于主塔冷量富裕，可开大液氧或液氮排放阀多排放液体氧、氮产品。
以上所述的实施例仅是对本发明的优选方式进行描述，并非对本发明的范围进行限定，在不脱离本发明设计精神的前提下，本领域普通技术人员对本发明的技术方案做出的各种变形和改进，均应落入本发明权利要求书确定的保护范围内。

Claims (4)

1.一种大型制氧机组氩系统变负荷方法，其特征在于，通过调节粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的方式达到大型制氧机组氩系统氩气增产、氩气减产目的；
其中氩气增产时具体粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的操作条件如下表：
粗氩流量 1500Nm3/h 1600Nm3/h 1700Nm3/h V701阀开度 20％一20.5％ 20.3％一20.6％ 20.5％一20.8％ 氩馏份氩含量 10～11％Ar 10.5～11.5％Ar 10.5～11.8％Ar
其中氩气减产时具体粗氩气流量、Ⅴ701阀开度和氩馏份氩含量的操作条件如下表：
Figure FDA0001904090460000011
所述Ⅴ701阀开度和氩馏份氩含量根据表中灵活控制，V701开度增大时氩馏份氩含量减小。
2.根据权利要求1所述的大型制氧机组氩系统变负荷方法，其特征在于，氩气减产时，Ⅴ3阀开度在0.2-0.5％。
3.根据权利要求1所述的大型制氧机组氩系统变负荷方法，其特征在于，氩气减产时，Ⅴ3阀开度在0.35％。
4.根据权利要求2所述的大型制氧机组氩系统变负荷方法，其特征在于，所述V3阀正常工作时开度为66％，膨胀量在23000-24000Nm3/h。
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