CN204027204U - 液氮辅助精馏空分设备 - Google Patents

液氮辅助精馏空分设备 Download PDF

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CN204027204U
CN204027204U CN201420286398.5U CN201420286398U CN204027204U CN 204027204 U CN204027204 U CN 204027204U CN 201420286398 U CN201420286398 U CN 201420286398U CN 204027204 U CN204027204 U CN 204027204U
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tower
condenser
argon
nitrogen
subcooler
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崔新亭
丁友胜
赵小莹
王亮
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ZOKO ENERGY EQUIPMENT CO Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Abstract

本实用新型涉及一种液氮辅助精馏空分设备。下塔顶部与主冷凝蒸发器的氮气进口和液氮出口接通；主冷凝蒸发器的液氮出口、过冷器、上塔顶部依次接通；下塔底部与过冷器接通；过冷器与上塔污氮气抽口接通；辅助冷凝器的液氮出口、过冷器、分离器的进料口依次接通；上塔底部与主换热器接通；上塔污氮气抽口、过冷器、主换热器依次接通；上塔顶部、过冷器、主换热器依次接通；辅助精馏塔的原料气进口和底部分别与下塔氮馏分抽口接通，辅助精馏塔顶部与辅助冷凝器的氮气进口接通，辅助精馏塔的回流液进口与辅助冷凝器的液氮出口接通。本实用新型结构设计合理、液氮产品和氮气产品纯度高。

Description

液氮辅助精馏空分设备
技术领域
本实用新型涉及一种液氮辅助精馏空分设备，属于空分领域。
背景技术
随着空分设备在化工行业的应用的增加和气体公司的增加，对产品纯度广泛出现了以下要求：
                          表1：空气分离产品新的需求。
满足以上条件的现有技术的空分设备精馏过程有以下缺点：1、液氮产品的纯度取决于下塔顶部的氮气纯度，其含氧量越低，下塔顶部获得的氮气越少，主冷凝蒸发器冷凝的液氮越少，能够向上塔顶部提供的液氮回流液越少，上塔的回流比也越差，氧气产品提取率越小，所需原料空气越多，能耗越高，液氮产品和氧气产品纯度低。2、下塔液氮在经过过冷后，如果以常压送出的话，其氧的含量还会增长约10%，更加影响液氮馏分的取出量。
实用新型内容
本实用新型的目的在于克服现有技术中存在的上述不足，而提供一种结构设计合理、液氮产品和氮气产品纯度高的液氮辅助精馏空分设备。
本实用新型解决上述问题所采用的技术方案是：一种液氮辅助精馏空分设备，包括主换热器、膨胀机、液氮气液分离器、过冷器、主精馏塔；主精馏塔包括下塔、上塔；在上塔的底部设置有主冷凝蒸发器和辅助冷凝器；膨胀机包括膨胀机增压端、膨胀机增压后冷却器、膨胀机膨胀端；主换热器与下塔的底部接通；膨胀机增压端、增压后冷却器、主换热器、膨胀机膨胀端、主精馏塔依次接通；下塔顶部与主冷凝蒸发器的氮气进口和液氮出口接通；主冷凝蒸发器的液氮出口、过冷器、上塔顶部依次接通；下塔底部与过冷器接通；过冷器与上塔污氮气抽口接通；辅助冷凝器的液氮出口、过冷器、分离器的进料口依次接通；上塔底部与主换热器接通；上塔污氮气抽口、过冷器、主换热器依次接通；上塔顶部、过冷器、主换热器依次接通；其特征在于：还包括辅助精馏塔；辅助精馏塔的原料气进口和底部分别与下塔氮馏分抽口接通，辅助精馏塔顶部与辅助冷凝器的氮气进口接通，辅助精馏塔的回流液进口与辅助冷凝器的液氮出口接通。
本实用新型还包括氩塔，氩塔内设有氩塔冷凝蒸发器；过冷器与氩塔冷凝蒸发器的冷凝测接通；氩塔冷凝蒸发器的液空侧与上塔液空进口接通；氩塔顶部与上塔液空进口接通；氩塔上部与氩塔冷凝蒸发器的氩侧接通；氩塔冷凝蒸发器的氩侧与氩塔的冷凝液回流口接通；氩塔冷凝蒸发器液氩抽口与上塔污氮气进口接通；上塔氩馏分抽口分别与氩塔的底部和氩馏分入口接通。
本实用新型与现有技术相比，具有以下优点和效果：
1、在下塔上部合适的位置，抽出部分氮气馏分，在辅助精馏塔内精馏，在顶部获得≤1ppmO2的氮气，进入辅助冷凝器，被液氧冷凝后部分返回辅助精馏塔参与精馏，部分去过冷器过冷后，经液氮气液分离器进行低压分离后，将符合要求的液氮产品送出空分设备。
2、辅助精馏塔所需要的塔板数少于其抽口以上的塔板数，其精馏负荷和下塔相比，所占比例极小，所以从结构上是可行的，增加设备成本极少，针对50000的空分设备来讲不超过20万元，针对表1中的工况2，原料空气节省1%以上。同时，空分设备其余环节均能保持原来的平衡状态，所以适用于各种流程形式的空分设备。
3、辅助精馏塔可使空分设备的精馏效果摆脱液氮产品的限制。例如，要获得≤1ppmO2的氮气产品，下塔顶部的液氮含氧量可达3ppm，去上塔的液氮回流流量可增加1.3%以上，这对氧的提取率改善极为有利；而此时通过辅助精馏塔获得的液氮产品纯度仍可以远优于≤1ppmO2的要求。
以一套氧气产量为22000Nm3/h的空分设备为例，其要求见表2：
表2 示例空分设备的产品要求。
1、不带辅助精馏塔时所需空气流量118600Nm3/h，液氩产量575Nm3/h；
2、采用辅助精馏塔时，所需空气流量117400 Nm3/h，液氩产量572Nm3/h。
经过对比，本实用新型可使原料空气流量降低1%，按进口压缩机性能计算，直接节省能耗约100KW，按每年工作8000小时计算，可减少耗电800000KW.H，折合费用约40万元以上，如果用于40000 Nm3/h等级以上的空分设备，节能效果更加明显。
如果氮气产品的要求更低，采用本实用新型，节能比例还会上升，这对气体公司来说，效益比较显著。
附图说明
图1为本实用新型实施例的结构示意图。
具体实施方式
下面结合附图并通过实施例对本实用新型作进一步的详细说明，以下实施例是对本实用新型的解释而本实用新型并不局限于以下实施例。
参见图1，本实用新型实施例包括主换热器E1、膨胀机、氩塔C3、辅助精馏塔C4、液氮气液分离器S1、过冷器E2。
主精馏塔包括下塔C1、上塔C2。在上塔C2的底部设置有主冷凝蒸发器K1和辅助冷凝器K2。氩塔C3上部设有氩塔冷凝蒸发器K3。膨胀机包括膨胀机增压端BT、膨胀机增压后冷却器WE、膨胀机膨胀端ET。
管路1中的原料空气向空分设备提供原料气，进冷箱前分为管路2中的原料空气和管路3中的膨胀空气两路。管路1中的原料空气为来自压缩机、经过预冷系统冷却、吸附系统净化后的压力空气。
主换热器E1与下塔C1的底部通过管路2接通。管路2中的原料空气经主换热器E1进入下塔C1底部，作为下塔C1精馏的原料气。
膨胀机增压端BT、增压后冷却器WE、主换热器E1、膨胀机膨胀端ET、上塔C2通过管路3依次接通。膨胀空气经膨胀机增压端BT、膨胀机增压后冷却器WE、主换热器E1、膨胀机膨胀端ET进入上塔C2，为空分设备的精馏提供冷量。此为内压缩流程，膨胀空气经膨胀机膨胀端ET后也可进入下塔C1底部。
下塔C1顶部与主冷凝蒸发器K1的氮气进口通过管路4接通。压力氮气由下塔C1顶部进入主冷凝蒸发器K1被冷凝，主冷凝蒸发器K1外侧的液氧被蒸发。
下塔C1顶部与主冷凝蒸发器K1的液氮出口通过管路5接通，主冷凝蒸发器K1的液氮出口、过冷器E2、上塔C2顶部通过管路5和管路6依次接通。管路5中的回流液氮在主冷凝蒸发器K1内被液氧冷凝后分两路，管路6的液氮去过冷器E2，然后进入上塔C2顶部，另一路返回下塔C1顶部，作为下塔C1精馏的回流液。
下塔C1底部与过冷器E2通过管路7接通；过冷器E2与上塔C2污氮气抽口下部通过管路14接通，过冷器E2与氩塔冷凝蒸发器K3的冷凝测通过管路15接通。上塔C1底部的富氧液空经过冷器E2过冷后，经管路14去上塔C2污氮气抽口下部作为上塔回流液，另一路经管路15去氩塔冷凝蒸发器K3的冷凝测，为氩塔C3的精馏提供冷源。
下塔C1上部的氮馏分抽口与辅助精馏塔C4底部的原料气进口通过管路8接通。由下塔C1上部抽出部分氮馏分进入辅助精馏塔C4底部作为液氮原料气。
辅助精馏塔C4底部与下塔C1氮馏分抽口通过管路9接通。辅助精馏塔C4底部回流液至下塔C1氮馏分抽口处，在下塔C1内继续参与精馏。
辅助精馏塔C4顶部与辅助冷凝器K2的氮气进口通过管路10接通。氮气由辅助精馏塔C4顶部去辅助冷凝器K2，被外侧液氧冷凝。
辅助冷凝器K2的液氮出口与辅助精馏塔C4上部的回流液进口通过管路11和管路12接通，辅助冷凝器K2的液氮出口、过冷器E2、分离器S1的进料口通过管路11和管路13依次接通。管路11中由辅助冷凝器K2回流的液氮，分两路，一路通过管路12返回辅助精馏塔C4上部作为回流液，一路通过管路13去过冷器E2过冷后，进入液氮气液分离器S1。
氩塔冷凝蒸发器K3的液空侧与上塔C2液空进口下部通过管路16接通。液空回流液出氩塔C3的冷凝蒸发器K3液空侧后回流到上塔C2液空进口下部。
氩塔C3顶部与上塔C2液空进口下部通过管路17接通。氩塔冷凝蒸发器K3的液空侧汽化后得到的液空蒸汽，返回上塔C2液空进口下部。
氩塔C3上部与氩塔冷凝蒸发器K3的氩侧通过管路18接通。氩塔C3上部的氩气进入氩塔冷凝蒸发器K3氩侧。
氩塔冷凝蒸发器K3的氩侧与氩塔C3的冷凝液回流口通过管路19接通。氩塔冷凝蒸发器K3氩侧的作为冷凝液的液氩回流液回流到氩塔C3。
氩塔冷凝蒸发器K3液氩抽口与上塔C2污氮气进口通过管路20接通。氩塔冷凝蒸发器K3液氩抽口封头处排放的含氮不凝气，进入上塔C2污氮气流路。含氮不凝气含N??≤1%。
上塔C2氩馏分抽口与氩塔C3底部通过管路22接通，上塔C2氩馏分抽口与氩塔C3底部的氩馏分入口通过管路21接通。上塔C2氩馏分抽口抽出的氩馏分，通过管路21进入氩塔C3底部作为上升蒸汽参与精馏。氩塔C3底部的氩馏分回流液，通过管路22经泵加压进入上塔C2的氩馏分抽口处，参与上塔C2的精馏。
上塔C2底部与主换热器E1通过管路23接通。来自上塔C2底部的氧气产品，经主换热器E1复热后作为产品送出空分设备系统。
上塔C2污氮气抽口、过冷器E2、主换热器E1通过管路24依次接通。来自上塔C2氮气产品气抽口下部的污氮气抽口的污氮气与来自氩塔冷凝蒸发器K3的不凝气汇合，经过冷器E2，主换热器E1复热后送出空分设备系统，出空分设备后，部分去纯化系统作为再生气，部分去预冷系统回收冷量。
上塔C2顶部、过冷器E2、主换热器E1通过管路25依次接通。来自上塔C2顶部的氮气，经过冷器E2，主换热器E1复热后送出空分设备系统。
来自主冷凝蒸发器K1和辅助冷凝器K2液氧侧的液氧通过管路26送出。
来自液氮气液分离器S1底部的液氮产品通过管路27送出。
来自氩塔C3底部上部的液氩产品通过管路28送出。
本实用新型各设备的作用如下：
主换热器E1：管路2中的原料空气、管路3中的膨胀空气在内部被氧气、污氮气、氮气返流气体冷却。
膨胀机增压端BT：管路3中的膨胀空气先在膨胀机增压端BT内增压，用来回收膨胀机膨胀端ET的膨胀功。与膨胀机膨胀端ET组成一个机组。
膨胀机增压后冷却器WE：膨胀机增压端BT出口的空气被冷却。
膨胀机膨胀端ET：对管路3中的膨胀空气降温降压。
下塔C1：管路2中的原料空气在主换热器E1内被冷却后，在下塔C1内进行初步分馏，顶部获得氮气，在主冷凝蒸发器K1内冷凝获得液氮，部分回流作为下塔C1回流液，其余部分作为上塔C2回流液。下塔C1顶部的液氮含氧量可高于产品液氮纯度的要求，这样可获得更多的液氮回流液去上塔C2，经过精馏作用后，在上塔C2顶部可获得满足要求的氮气产品。这样，改善上塔C2回流比后，可提高产品提取率，减少空气用量，起到节能作用。
上塔C2：将来自下塔C1、膨胀机膨胀端ET、氩塔C3的液体和气体物流在低压下进行再次分馏，获得合格的氮气、氧产品和液氧产品，同时向氩塔C3提供氩馏分，并与氩塔C3进行其它物流连接，保证氩塔系统平稳运行。如果不需要氩产品，就没有和氩系统连接的物流。如果膨胀空气进下塔，其所有物流来自下塔C1、氩塔C3。
过冷器E2：通过来自上塔C2的氮气、污氮气将下塔C1去上塔C2的物流进行过冷，改善上塔C2的精馏工况，将来自辅助精馏塔C4的液氮产品过冷，减少液氮产品的汽化。必要的时候，液氧产品也可在过冷器E2内获得一定的过冷度。
氩塔C3：将来自上塔C2的氩馏分进行分离，获得合格的液氩产品。其通过精馏部分和辅助冷凝器K2的各部分物流和上塔C2连接起来，以便稳定运行，获得合格的氩产品。本实用新型的氩塔C3为组合功能，可直接获得液氩产品，氩塔C3分为粗氩塔和精氩塔。
液氮气液分离器S1：来自辅助冷凝器K2的管路13内的液氮在过冷器E2内过冷后，在液氮气液分离器S1内进行低压分离，获得低压稳定的液氮产品。
主冷凝蒸发器K1：下塔C1顶部的氮气被冷凝成液氮，上塔C2底部的液氧被蒸发。
辅助冷凝器K2：辅助精馏塔C4顶部的氮气被冷凝成液氮，上塔C2底部的液氧被蒸发。液氮纯度与液氮产品纯度要求相同，部分被送出，经过冷和分离后作为产品送出。
氩塔冷凝蒸发器K3：氩塔C4顶部的氩气被冷凝，来自过冷器E2的液空被汽化。为氩塔的精馏提供冷量。
本实用新型中涉及的装置及部件的名称、结构、功能均能为本领域技术人员理解。
此外，需要说明的是，本说明书中所描述的具体实施例，其零、部件的形状、所取名称等可以不同，本说明书中所描述的以上内容仅仅是对本实用新型结构所作的举例说明。 

Claims (2)

1.一种液氮辅助精馏空分设备，包括主换热器、膨胀机、液氮气液分离器、过冷器、主精馏塔；主精馏塔包括下塔、上塔；在上塔的底部设置有主冷凝蒸发器和辅助冷凝器；膨胀机包括膨胀机增压端、膨胀机增压后冷却器、膨胀机膨胀端；主换热器与下塔的底部接通；膨胀机增压端、增压后冷却器、主换热器、膨胀机膨胀端、主精馏塔依次接通；下塔顶部与主冷凝蒸发器的氮气进口和液氮出口接通；主冷凝蒸发器的液氮出口、过冷器、上塔顶部依次接通；下塔底部与过冷器接通；过冷器与上塔污氮气抽口接通；辅助冷凝器的液氮出口、过冷器、分离器的进料口依次接通；上塔底部与主换热器接通；上塔污氮气抽口、过冷器、主换热器依次接通；上塔顶部、过冷器、主换热器依次接通；其特征在于：还包括辅助精馏塔；辅助精馏塔的原料气进口和底部分别与下塔氮馏分抽口接通，辅助精馏塔顶部与辅助冷凝器的氮气进口接通，辅助精馏塔的回流液进口与辅助冷凝器的液氮出口接通。
2.根据权利要求1所述的液氮辅助精馏空分设备，其特征在于：还包括氩塔，氩塔内设有氩塔冷凝蒸发器；过冷器与氩塔冷凝蒸发器的冷凝测接通；氩塔冷凝蒸发器的液空侧与上塔液空进口接通；氩塔顶部与上塔液空进口接通；氩塔上部与氩塔冷凝蒸发器的氩侧接通；氩塔冷凝蒸发器的氩侧与氩塔的冷凝液回流口接通；氩塔冷凝蒸发器液氩抽口与上塔污氮气进口接通；上塔氩馏分抽口分别与氩塔的底部和氩馏分入口接通。
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Publication number Priority date Publication date Assignee Title
CN104949471A (zh) * 2015-05-14 2015-09-30 马钢(集团)控股有限公司 一种提高空分装置氮气产量的方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104949471A (zh) * 2015-05-14 2015-09-30 马钢(集团)控股有限公司 一种提高空分装置氮气产量的方法

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