CN1340687A - 空气分离方法及设备 - Google Patents

空气分离方法及设备 Download PDF

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Publication number
CN1340687A
CN1340687A CN00128025A CN00128025A CN1340687A CN 1340687 A CN1340687 A CN 1340687A CN 00128025 A CN00128025 A CN 00128025A CN 00128025 A CN00128025 A CN 00128025A CN 1340687 A CN1340687 A CN 1340687A
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gas
condenser
pressure column
column
pressure
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CN00128025A
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孙克锟
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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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/04181—Regenerating the adsorbents
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
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    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
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    • 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
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    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • 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
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/70—Heating the adsorption vessel
    • 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
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • 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
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Abstract

本发明属于低温精馏空气分离的领域,应用低温精馏的原理分离空气以制取氧、氮、氩气的方法及设备。它在很低的能耗条件下,通过单级精馏设备制取含氧为5%～3ppm的纯氮产品,还能制取含氧为40～99.5%的富氧或纯氧产品,或者通过双级精馏设备制取含氧85～99.999%的氧产品和含氧为2%～3ppm的压力纯氮产品。压力塔附设一只粗氩塔或精氩塔制取粗氩或纯氩。对氧、氮、氩均有极高的提取率。

Description

空气分离方法及设备
本发明属于低温精馏空气分离的领域，应用低温精馏的原理分离空气，制取氧、氮、氩的方法和设备。
传统的单级精馏塔流程，一般仅能制取单一的富氧或纯氮气体，产品提取率低，若要制取更多的产品气，必须通过增加压力的方法，并且工艺流路复杂。相应能耗也较高。传统的双级精馏塔流程，制取纯氧和低压氮气时，塔板多，体积大，能耗高。
鉴于上述公知的技术不足，本发明的任务是提出一种改进的空气分离方法及设备，它在较低的能耗条件下，通过单级精馏设备制取含氧为5％～3ppm氮产品，还能制取含氧为40～99.5％的富氧或纯氧产品，或者通过双级精馏设备制取含氧85～99.999％的氧产品，和含氧为2％～3ppm的压力纯氮产品。压力塔附设一只精氩塔制取氩气，压力塔附设一只粗氩塔制取粗氩。对氧、氮，氩气均有极高的提取率。
本发明的任务是用下列方法来解决的：一种单级低温精馏的空气分离方法，其特征在于在压力塔底部设置一只蒸发器，在压力塔顶部设置一只冷凝器和在压力塔内还可设置有辅助冷凝器组，被压缩的原料空气冷却排水后，在空气预冷器冷却除水后进入分子筛吸附器中除去微量水份、二氧化碳、乙炔及其他部分碳氢化合物形成净化原料空气，在主换热器内冷却后的部分原料空气进入压力塔底部的蒸发器中，作加热气源加热液体空气，被冷却液化后的原料空气出蒸发器后与另一部分原料空气在过冷器中冷却汇合，经减压降温后进入压力塔中部。从主换热器内引出一部分压力空气进入膨胀机绝热膨胀再冷却后进入压力塔中部参与精馏。本发明的空气分离设备流程为增压膨胀流程，从压力塔内的精馏段引出的压力不纯氮气体复热至常温后，在增压机中增压后在主换热器内冷却至一定温度后，进入膨胀机中作绝热膨胀。
本发明所制取的氧氮产品(包括富氧)的压力有着较宽的范围，当产品气压力低于压力塔工作压力时，可从压力塔顶冷凝器内引出部分富氧(纯氧)液体，或从压力塔顶引出部分液氮，分别进入压力塔精馏段内所设置的辅助冷凝器内，被塔内上升蒸气所蒸发，再经换热器组复至常温后出装置；当产品气压力高于压力塔工作压力时，所引的富氧(纯氧)液体或液氮被低温液体泵所压缩，被压缩后的液体温度和焓值低于塔内相应部位上升蒸气的温度和焓值时，形成一定的温差和焓差时，压缩后的低温液体可进入塔内所设置在该部位下方的辅助冷凝器内，压缩后的低温液体被塔内上升蒸气所汽化，再经换热器组复至常温后出装置。
必须指出：单级低温精馏的空气分离流程制取富氧的最佳范围在70—75％内时能耗最低。同时必须严格控制压力塔内压力氮气、低温液氮和压力不纯氮气三者之和一般不得大于精馏段内上升蒸气总量的50％，以保证精馏段内的回流比不低于0.5。
一种低温精馏的空气分离方法，采用双级精馏塔的流程时，它基于单级塔流程，通过压力塔所获得的纯液氮减压降温后进入低压塔顶冷凝器低压侧作低压塔的冷源，压力塔顶冷凝蒸发器作为低压塔的热源，在低压塔中精馏分离来自压力塔釜的富氧液空，低压塔底部可获得纯氧。
在塔内均设有塔板段或填料物。
为了同时制取高纯氮产品和纯氧气，必须在单塔中具有制取粗氩或精氩的能力，粗氩或精氩的提取改善了压力塔的精馏工况。
本发明的任务是用下列空气分离设备来解决的。
一种单级精馏塔的空气分离设备流程，其特征为：
a.被压缩的原料空气在空气预冷器冷却除水后，再进入分子筛吸附器中除去微量水份，二氧化碳，乙炔及其他部分碳氢化合物形成净化原料空气。
b.净化原料空气进入主换热器后分成二部分，从主换热器内引出部分原料空气进入精馏塔底部的蒸发器内加热釜中的液体空气，被冷却液化后的原料空气与另一部分原料空气在过冷器中冷却汇合后，经减压降温后进入精馏塔中部。
c.从主换热器内引出一部分压力原料空气绝热膨胀后，进入精馏塔中部参与精馏。
d.精馏塔顶部设置一只冷凝器，从精馏塔底部引出的富氧液体在过冷器中过冷后，再经减压降温后进入塔顶冷凝器内作塔的冷源，蒸发气体再经换热器组复热后作产品气。从压力塔顶部引出压力氮气在换热器组复热至常温后作产品气。
e.从压力塔精馏段引出的压力不纯氮气，在换热器组复至常温后进入增压机中增压，再在主换热器内冷却至一定温度后进入膨胀机作绝热膨胀的，膨胀气体则进入过冷器和换热器组复热出装置，一部分气体进入分子筛吸附器作再生气体。
f.可从冷凝器内引出一部分液氧，进入精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者部分液氧经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源。蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
g.可从精馏塔顶引出一部分纯液氮，经减压降温后进入精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氮经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源，蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
一种双级精馏塔的空气分离设备的空气分离流程，其特征为：
a.被压缩的原料空气在空气预冷器冷却除水后，再进入分子筛吸附器中除去微量水份、二氧化碳、乙炔及其他部分碳氢化合物形成净化原料空气。
b.净化原料空气进入主换热器后分成二部分，从主换热器内引出部分原料空气进入精馏塔底部的蒸发器内加热塔釜中的液体空气，被冷却液化后的原料空气与另一部分原料空气在过冷器中冷却汇合后，经减压降温后进入压力塔中部。
c.从主换热器引出一部分压力原料空气绝热膨胀后，进入精馏塔中部参与精馏。
d.从压力塔底部所引出的富氧液体空气，经一只过冷器被出塔的返流气体过冷后，再经一只减压阀减压降温后进入低压塔中部进行再次精馏。
e.从压力塔顶部所引出的部分液氮被过冷器过冷后，经减压降温后进入低压塔顶部冷凝器作冷源。从低压塔顶部冷凝器所蒸发的低压氮气经一只过冷器复热后，再进入换热器组复热至常温后作产品气。
f.从压力塔顶部所引出的氮气经换热器组复热后引出装置作纯氮产品气，在低压塔底部冷凝器中获得液氧产品；在低压塔底冷凝器上部引出高纯氧气经换热器组复热至常温后作产品气；在低压塔顶部冷凝器气氮侧和压力塔顶部可获得纯液氮产品。
g.从压力塔精馏段引出的压力不纯氮气，在换热器组复热至常温后进入增压机中增压，然后进入主换热器内冷却至一定温度后再进入膨胀机作绝热膨胀的，膨胀气体再进入过冷器和换热器组复热出装置，一部分气体进入分子筛吸附器作再生气体。
h.可从压力塔顶部冷凝器内引出一部分液氧，进入压力塔精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氧经一只低温液体泵压缩至一定压力后，进入压力塔内适当部位所设置的辅助冷凝器作冷源。蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
i.可从低压塔顶部冷凝器引出一部分纯液氮，进入压力塔精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氮经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源，蒸发气体再在换热器组复热作产品气，或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
空分压力塔附设一只粗氩塔的空气分离设备流程，其特征：
a.粗氩塔由压力塔和冷凝器组成。在压力塔顶部设置一只冷凝器，由空分压力塔原料空气入口处下部，所设置的提馏段中部的氩馏份富集区引出一部分氩馏份气体，进入精氩塔的压力塔下部作原料气。
b.原料气在粗氩塔内精馏分离后，在塔底所得的富氧液体仍回入空分压力塔相应部位，在粗氩冷凝器内排出少量废气。在粗氩塔顶部引出粗氩气体。
c.引入来自空分压力塔项部冷凝器内部分富氧液体空气进入粗氩塔顶部的冷凝器中作塔的冷源，蒸发气体出塔经复热后出装置。
空分压力塔附设一只精氩塔的空气分离设备流程，其特征：
a.在精氩塔的压力塔顶部设置一只冷凝器，由空分压力塔原料空气入口处下部，所设置的提馏段中部的氩馏份富集区引出一部分氩馏份气体，进入精氩塔的压力塔下部作原料气。
b.原料气在压力塔内精馏分离后，在塔底所获得的富氧液体，仍回入空分压力塔相应部位，在压力塔顶部获得的粗氩液体，经减压降温后进入低压塔中部进行再次精馏。
c.引入来自空分压力塔顶部的纯液氮进入压力塔顶部冷凝器作冷源，被蒸发的气氮在冷却器冷却液化后，再经减压降温后进入低压塔顶部的冷凝器中作塔的冷源，蒸发氮气出塔经复热后作产品气。
d.液氩在低压塔精馏后，在低压塔顶部排出少量废气，在低压塔下部冷凝器获得精氩液体或精氩气体产品。
双级精馏塔附设一只精氩塔的空气分离设备流程，其特征：
a.精氩塔由压力塔和低压塔组成，中间设置一只冷凝蒸发器，在低压塔顶部设置一只冷凝器，由空分压力塔净化原料空气入口处下部，所设置的提馏段中部的氩馏份富集区引出一部分氩馏份气体，进入精氩塔的压力塔下部作原料气。
b.原料气在压力塔内精馏分离后，在塔底所获得的富氧液体，仍回入空分压力塔相应部位，在压力塔顶部获得的粗氩液体，经减压降温后进入低压塔中部进行再次精馏。
c.引入来自空分压力塔顶部主冷凝器内的部分液氧，进入精氩压力塔顶部冷凝器作冷源，被蒸发的气氧出冷凝器后与空分主冷凝器所引出的气氧汇合，复热至常温后出装置作产品气。
d.引入来自空分低压塔顶部冷凝器内的低压纯液氮，进入精氩低压塔顶部冷凝器作冷源，被蒸发的气氮出冷凝器后与空分低压塔顶部冷凝器作蒸发的气氮汇合后，复热至常温后出装置作产品气。
e.液氩在低压塔精馏后，在低压塔顶部排出少量废气，在低压塔下部冷凝器获得精氩液体或精氩气体产品。
下面结合流程图，描述各种空气分离设备流程。
图1一种单级精馏塔的空气分离设流程。
图2一种双级精馏塔的空气分离设流程。
图3空分压力塔附设一只精氩塔的空气分离设备流程。
图4空分压力塔附设一只精氩塔的空气分离设备流程。
图5双级精馏塔压力塔附设一只粗氩塔的空气分离设备流程。
图1是精馏塔为一只压力塔的空气分离设备流程。
图1(a)是精馏塔为一只压力塔的空气分离设备流程。原料空气由管道1进入压缩机2压缩冷却排水后，由管道3在空气预冷器4冷却后除水后，经管道5，进入分子筛吸附器6除去微量水份、二氧化碳、乙炔及其他碳氢化合物，经管道7、主换热器8被返流气体所冷却，从主换热器8内引出的部分原料空气经管道9、阀门10、管道11、进入精馏塔12底部蒸发器13中作加热气体，被富氧液空冷却液化后的压力原料空气由管道15引出，与另一部分原料空气经管道24汇合进入过冷器16被进一步冷却后，经管道17减压阀18减压降温后，经管道19进入精馏塔12中部，原料空气入塔段下部，序号12a为精馏塔的提馏段。精馏塔12顶部设有冷凝器14，塔内上升气体被上部冷凝器所冷凝，在塔内产生足够的回流液时，在塔顶冷凝器冷量有富裕时，可从塔顶所冷凝的部分纯液氮引出经管道31，减压阀32减压降温后，管道33进入主冷凝器14作塔的冷源。从主换热器内引出一部分压力原料空气由管道20引出，进入膨胀机21中作绝热膨胀，膨胀气体由管道22，在过冷器16冷却后进入压力塔中部参与精馏。此流路也可以是增压膨胀形式(附图中均未绘出)。
在塔釜引出含氧大于50％的压力富氧液体经管道25进入过冷器16、27过冷后，经管道28，减压阀29减压降温后，由管道30进入冷凝器14中作压力塔的冷源。蒸发气体由管道55引出，在过冷器27、16、主换热器8，预冷器4复热后，在管道57引出作富氧产品，由冷凝器14中的氮通道引出所蒸发的氮气由管道34引出经过冷器27和16，主换热器8，空气预冷器4复热后作纯氮气产品。从压力塔12精馏段引出含氧不高于5％的压力不纯氮气，经管道42，换热器组27、16、8复热至一定温度后由管道44进入增压器46中增压后，经管道47进入主换热器8冷却至一定温度后进入膨胀机49内作绝热膨胀，膨胀气体由管道50引出，进入过冷器27、16和主换热器8，空气预冷器4复热至常温，大部分不纯氮气由管道53进入分子筛吸附器6作再生气体，再由管道54放空。必须严格控制压力塔内压力氮气、低温液氮和压力不纯氮气三者之和一般不得大于精馏段内上升蒸气总量的50％，以保证精馏段内的回流比不低于0.5。从冷凝器14引出的低压氮气经管道34，过冷器27、16和主换热器8，空气预冷器4复热至常温后作低压纯氮气产品。从压力塔12顶部引出部分压力纯氮气由管道39引出，进入过冷器27，16和主换热器8，空气预冷器4复热至常温后，由管道41引出作压力纯氮气产品。从管道38引出少量纯液氮产品。从冷凝器14引出部分富氧液体经管道60，阀门61，管道62进入精馏段内辅助冷凝器63作冷源，以增加压力不纯氮气出口下部精馏段的回流液，复热的气体后经管道64进入低压氧气管道55中汇合。
图1(b)是单级精馏塔带有低温泵的空气分离设备流程。即从冷凝器14引出部分液氧经管道60，低温泵65加压后，当被低温液体泵压缩后的液体温度和焓值低于塔内某一截面上升蒸气的温度和焓值，形成一定的温差和焓差时，压缩后的低温液体可由管道66、69进入塔内该截面下部所设置的辅助冷凝器70内，被塔内上升蒸气所复热，由管道76引出，进入过冷器16内的压力氧通道内。当被低温液体泵压缩后的液体压力较高时，且焓值大于塔内各部位上升蒸气的温度和焓值时，这部分低温液体进入过冷器16主换热器8，空气预冷器4复热至常温作压力产品气。
图1(c)是精馏塔为一只压力塔的空气分离设备流程。在塔顶所冷凝的部分液氮引出经管道31，减压阀32减压降温后，从管道33进入主冷凝器14作塔的冷源。可从管道33引出部分低温液氮进入塔内所设置进入塔内所设置的辅助冷凝器63内作冷源，复热后经管道64进入低压氮气管道35中汇合。
图1(d)是单级精馏塔带有低温泵的空气分离设备流程。即从冷凝器14引出部分液氮经管道72，低温泵73加压后，当被低温液体泵压缩后的液体温度和焓值低于塔内某一截面上升蒸气的温度和焓值，形成一定的温差和焓差时，压缩后的低温液体可由管道74、75进入塔内该截面下部所设置的辅助冷凝器70内，被塔内上升蒸气所复热，由管道76引出，进入过冷器16内的压力氮通道内。当被低温液体泵压缩后的液体压力较高时，且温度和焓值大于塔内各部位上升蒸气的温度和焓值时，这部分低温液体进入过冷器16主换热器8，空气预冷器4复热至常温作压力气氮产品。
图2一种双级精馏塔的空气分离设备流程。
图2(a)是原料空气由管道1进入压缩机2压缩冷却排水后，由管道3在空气预冷器4冷却除水后，经管道5进入分子筛吸附器6除去微量水份、二氧化碳、乙炔及其他部分碳氢化合物，经管道7进入主换热器8所冷却，从主换热器内引出的部分原料空气经管道9，阀门10进入压力塔12蒸发器13内，加热塔釜内的富氧液体空气，原料空气被冷却液化后由管道15引出，与另一部分原料空气经管道24汇合进入过冷器16中被进一步冷却后，经管道17减压伐18减压降温后管道19再进入压力塔12中部。
在塔釜获得含氧大于60％的富氧液体由管道25引出，进入过冷器16、27被返流气体过冷后，经管道28减压阀29减压后由管道30进入低压塔31中部。从主换热器6内引出一部分压力原料空气由管道20引出，进入膨胀机21中作绝热膨胀，膨胀气体由管道22，在过冷器16冷却后进入压力塔中部参与精馏。此流路也可以是增压膨胀形式(附图中均未绘出)。压力塔12内上升气体被塔顶冷凝器14所冷凝，在塔内产生足够的回流液，由冷凝器14所冷凝的一部分纯液氮经管道33，换热器27经管道34减压阀35减压到不低于120KPa压力后，由管道36进入低压塔31顶部冷凝器32的冷源，必须保证冷凝器33二侧有一定的压力差来获得所需的冷凝温差冷凝上升气体中氧。低压塔31上部冷凝器32所蒸发的气氮经由管道59引出，经过冷器27、16、主换热器8，空气预冷器4复热至常温，由管道62引出装置。低压塔31顶部引出少量气体经管道56，经过冷器27、16主换热器8，空气预冷器4复热至常温后出装置。在压力塔12顶部获得的氮气由管道53引出，在过冷器16主换热器8复热至常温，由管道55获得压力氮气产品出装置。在冷凝蒸发器14上部被蒸发的含氧为85～99.999％气氧经管道65，过冷器27、16，主换热器8空气预冷器4复热至常温出装置，由管道67引出产品氧气。从压力塔12的精馏段由管道35引出部分含氧不高于5％的压力不纯氮气经换热器16，8复热至一定温度后由管道42引出进入增压机44增压后，经管道45在主换热器8冷却至一定温度由管道46进入膨胀机47作绝热膨胀，从管道48引出的膨胀气体，再经过冷器27、16和主换热器8空气预冷器4复热后由管道50引出，由管道51引出大部分低压不纯氮气进入分子筛吸附器6作再生气体，再由管道52放空。从压力塔12顶部冷凝器14引出部分液氧经管道68，阀门69，管道70进入压力塔12内压力不纯氮气管道40下部设置一只辅助冷凝器71内作塔的冷源，以增加压力不纯氮气出口下部精馏段的回流液，复热后经管道72进入低压氧气管道65中汇合，复热至常温出装置。必须严格控制压力塔内压力氮气、低温液氮和压力不纯氮气三者之和一般不得大于精馏段内上升蒸气总量的50％，以保证精馏段内的回流比不低于0.5。
图2(b)是双级精馏塔带有低温泵的空气分离设备流程。即从冷凝器14引出部分液氧经管道68，低温泵73加压后，当被低温液体泵压缩后的液体温度和焓值低于压力塔内某一截面上升蒸气的温度和焓值，形成一定的温差和焓差时，压缩后的低温液体可由管道74，77进入塔内该截面下部所设置的辅助冷凝器78内，被塔内上升蒸气所复热，由管道79引出，进入过冷器16内的压力氧通道内。当被低温液体泵压缩后的液体压力较高时，且温度和焓值大于塔内各部位上升蒸气的温度和焓值时，这部分低温液体进入过冷器16主换热器8，空气预冷器4复热至常温作压力产品气。
图2(c)是双级精馏塔的空气分离设备流程。在低压塔31顶冷凝器32所冷凝的部分液氮引出经管道80，阀门83，管道84进入塔内所设置的辅助冷凝器71内作冷源，复热后经管道85进入低压氮气管道35中汇合。
图2(d)是双级精馏塔带有低温泵的空气分离设备流程。即从低压塔31顶冷凝器32所冷凝的部分液氮引出经管道80低温泵81加压后，当被低温液体泵压缩后的液体温度和焓值低于压力塔内某一截面上升蒸气的温度和焓值，形成一定的温差和焓差时，压缩后的低温液体可由管道82，86进入塔内该截面下部所设置的辅助冷凝器78内，被塔内上升蒸气所复热，由管道87引出，进入过冷器16内的压力氮通道内。当被低温液体泵压缩后的液体压力较高时，且温度和焓值大于塔内各部位上升蒸气的温度和焓值时，这部分低温液体进入过冷器16主换热器8，空气预冷器4复热至常温作压力气氮产品。
图3是空分压力塔附设一只粗氩塔的空气分离设备流程。
与上述流程相比其变动部分是增加粗氩系统流程，介绍如下：
粗氩塔的流路中粗氩塔90顶部设有一只冷凝器91，从空分压力塔原料空气入口管道19下部所设置的提馏段12a中氩富集区，引出一股氩馏份气体经管道92进入粗氩塔90下部，上升气体中的氧被粗氩冷凝器91冷凝后，其回流液仍由管道93回入压力塔12a内，从管道95阀门96引出的一部分液氧，进入粗氩塔冷凝器91内作塔的冷源，被蒸发的气体由管道99回入管道55内，粗氩塔90顶部冷凝器91内由管道98排出少量废气，粗氩则从粗氩塔90顶部由管道94引出。
本图仅涉及设置粗氩塔后与空分压力塔有关流路，粗氩塔的设置适用于其他附图。(包括双级精馏塔的空气分离设备流程。)
图4是空分压力塔附设一只精氩塔的空气分离设备流程。
精氩系统流程介绍如下：
精氩塔由压力塔90和低压塔97组成，在压力塔90与低压塔97之间设置一只冷凝蒸发器91，在精氩塔的低压塔97顶部设有一只冷凝器98，从空分压力塔12的原料空气入口管道19下部所设置的提馏段12a氩富集区引出一股氩馏份气体，经管道92进入精氩塔的压力塔90下部，上升气体中的氧被冷凝后，其回流液仍由管道93回入空分压力塔12内，在压力塔90顶部被冷凝的粗氩液体经管道94引出，再在过冷器27过冷后，经减压阀95减压降温后，由管道96进入低压塔97中部进行再次精馏分离，从空分压力塔12顶部引出一部分压力液氮经管道31经减压阀101管道102进入冷凝器91作压力塔90的冷源，由管道103引出的气氮再在过冷器27冷凝后，经管道104，减压阀105减压降温后，由管道106进入精氩塔的低压塔97顶部冷凝器98内作低压塔的冷源，精氩塔顶部冷凝器98由管道109排出少量废气；在低压塔97顶部冷凝器98中，被蒸发的气体由管道111引出，进入低压氮气管道55中汇合，复热后出装置，精液氩则从精氩压力塔90顶部冷凝器91由管道110引出。
本图仅涉及设置精氩塔后与空分压力塔有关流路，精氩塔的设置适用于其他附图。(包括双级精馏塔的空气分离设备流程。)
图5是双级精馏塔附设一只精氩塔的空气分离设备流程。
与图4相比其变动部分是，引入来自空分压力塔顶部主冷凝器14内的部分液氧，经管道68，阀门106，管道107进入精氩压力塔顶冷凝器91内作压力塔90的冷源，被蒸发的气氧由管道108引出与空分主冷凝器14所引出的气氧汇合，进入管道65中，复热后出装置作产品气。引入来自空分低压塔顶部冷凝器32内的部份低压液氮，经管道80，阀门103，管道104进入精氩塔顶部冷凝器98内作低压塔97的冷源，被蒸发的气氮由管道111引出，进入空分塔顶部冷凝器32所蒸发的低压气氮汇合，经复热后出装置所产品气。由管道109引出少量塔顶的废气。
本图仅涉及设置精氩塔后与空分塔有关流路。

Claims (7)

1，一种单级低温精馏的空气分离方法，被压缩的原料空气冷却除水后，进入分子筛吸附器中除去微量水份、二氧化碳、乙炔及其他部分碳氢化合物形成净化原料空气，其特征在于在压力塔底部设置一只蒸发器，通入一部分净化原料空气作塔的热源，被冷却后的原料空气与另一部分原料空气通过换热器组冷却液化并汇合后，经减压降温后进入压力塔中部进行精馏分离；在压力塔顶部设置一只冷凝器冷凝塔内上升蒸汽；从压力塔精馏段引出一部分不纯氮气体经换热器组复热至一定温度后作膨胀气体，并作装置的冷源；还可通入低温液氧或液氮进入塔内所设置的辅助冷凝器组内作塔的冷源。
一种双级精馏塔的空气分离设备流程，它以单级塔流程为基础的，在低压塔顶部设置一只冷凝器，压力塔顶部的冷凝蒸发器作为低压塔的热源，精馏低压塔内的富氧液体或纯氧液体。
2、根据权利要求1所述的空气分离方法，其特征在于精氩塔由压力塔和低压塔组成，中间设置一只冷凝蒸发器，低压塔顶部设置一只冷凝器，由空分压力塔净化原料空气入口处下部所设置的提馏段的氩馏份富集区引出一部分氩馏份气体，通入精氩塔的压力塔底部作原料气，压力塔顶部被冷凝的粗液氩经减压降温后进入低压塔中部进行再次精馏分离，压力塔底部的冷凝液体仍回入压力塔内相应部位。引出压力塔顶部的部分冷凝液氮减压降温后进入精氩压力塔顶部冷凝器内作塔的冷源，或者引出空分塔主冷凝器的液氧作精氩压力塔顶冷凝器的冷源。设置在精氩塔的低压塔顶部的冷凝器内通入来自空分压力塔顶部所冷凝的液氮进入精氩塔的压力塔顶部冷凝器作冷源，出冷凝器后进入精氩塔的底压塔上冷凝器内作底压塔的冷源，或引入空分低压塔顶冷凝器的低压液氮作低压塔的冷源，精氩液体则在低压塔下部冷凝器引出，分别在压力塔顶部冷凝器和低压塔顶部冷凝器排出少量废气。
3.一种单级精馏塔的空气分离设备流程，其特征为：
a.被压缩的原料空气在空气预冷器冷却除水后，再进入分子筛吸附器中除去微量水份，二氧化碳，乙炔及其他部分碳氢化合物形成净化原料空气。
b.净化原料空气进入主换热器后分成二部分，从主换热器内引出部分原料空气进入精馏塔底部的蒸发器内加热釜中的液体空气，被冷却液化后的原料空气与另一部分原料空气在过冷器中冷却汇合后，经减压降温后进入精馏塔中部。
c.从主换热器内引出一部分压力原料空气绝热膨胀后进入精馏塔中部参与精馏。
d.精馏塔顶部设置一只冷凝器，从精馏塔底部引出的富氧液体在过冷器中过冷后，再经减压降温后进入塔顶冷凝器内作塔的冷源，蒸发气体再经换热器组复热后作产品气。从压力塔顶部引出压力氮气在换热器组复热至常温后作产品气。
e.从压力塔精馏段引出的压力不纯氮气，在换热器组复至常温后进入增压机中增压，再在主换热器内冷却至一定温度后进入膨胀机作绝热膨胀的，膨胀气体则进入过冷器和换热器组复热出装置，一部分气体进入分子筛吸附器作再生气体。
f.可从冷凝器内引出一部分液氧，进入精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者部分液氧经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源。蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
g.可从精馏塔顶引出一部分纯液氮，经减压降温后进入精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氮经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源，蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
4.一种双级精馏塔的空气分离设备的空气分离流程，其特征为：
a.被压缩的原料空气在空气预冷器冷却除水后，再进入分子筛吸附器中除去微量水份、二氧化碳、乙炔及其他部分碳氢化合物形成净化原料空气。
b.净化原料空气进入主换热器后分成二部分，从主换热器内引出部分原料空气进入精馏塔底部的蒸发器内加热塔釜中的液体空气，被冷却液化后的原料空气与另一部分原料空气在过冷器中冷却汇合后，经减压降温后进入压力塔中部。
c.从主换热器引出一部分压力原料空气绝热膨胀后，进入精馏塔中部参与精馏。
d.从压力塔底部所引出的富氧液体空气，经一只过冷器被出塔的返流气体过冷后，再经一只减压阀减压降温后进入低压塔中部进行再次精馏。
e.从压力塔顶部所引出的部分液氮被过冷器过冷后，经减压降温后进入低压塔顶部冷凝器作冷源。从低压塔顶部冷凝器所蒸发的低压氮气经一只过冷器复热后，再进入换热器组复热至常温后作产品气。
f.从压力塔顶部所引出的氮气经换热器组复热后引出装置作纯氮产品气，在低压塔底部冷凝器中获得液氧产品；在低压塔底冷凝器上部引出高纯氧气经换热器组复热至常温后作产品气；在低压塔顶部冷凝器气氮侧和压力塔顶部可获得纯液氮产品。
g.从压力塔精馏段引出的压力不纯氮气，在换热器组复热至常温后在增压机中增压，然后进入主换热器内冷却至一定温度后再进入膨胀机作绝热膨胀的，膨胀气体再进入过冷器和换热器组复热出装置，一部分气体进入分子筛吸附器作再生气体。
h.可从压力塔顶部冷凝器内引出一部分液氧，进入压力塔精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氧经一只低温液体泵压缩至一定压力后，进入压力塔内适当部位所设置的辅助冷凝器作冷源。蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
i.可从低压塔顶部冷凝器引出一部分纯液氮，进入压力塔精馏段不纯氮气出口处下部所设置的辅助冷凝器内作冷源，或者这部分液氮经一只低温液体泵压缩至一定压力后，进入塔内适当部位所设置的辅助冷凝器作冷源，蒸发气体再在换热器组复热作产品气。或者这部分低温液体经低温液体泵加压到较高压力后，则直接经换热器组复热后作压力产品气。
5.空分压力塔附设一只粗氩塔的空气分离设备流程，其特征：
a.粗氩塔由压力塔和冷凝器组成。在压力塔顶部设置一只冷凝器，由空分压力塔原料空气入口处下部所设置的提馏段中部的馏份富集区引出一部分氩馏份气体，进入粗氩塔下部作原料气。
b.原料气在粗氩塔内精馏分离后，在塔底所得的富氧液体仍回入空分压力塔相应部位，在粗氩冷凝器内排出少量废气。在粗氩塔顶部引出粗氩气体。
c.引入来自空分压力塔项部冷凝器内部分富氧液体空气进入粗氩塔顶部的冷凝器中作塔的冷源，蒸发气体出塔经复热后出装置。
6.空分压力塔附设一只精氩塔的空气分离设备流程，其特征：
精氩塔的压力塔顶部设置一只冷凝器，由空分压力塔净化原料空气入口处下部所设置的提馏段中部的氩馏份富集区引出一部分氩馏份气体，进入精氩塔的压力塔下部作原料气。
b.原料气在压力塔内精馏分离后，在塔底所获得的富氧液体，仍回入空分压力塔相应部位，在压力塔顶部获得的粗氩液体，经减压降温后进入低压塔中部进行再次精馏。
c.引入来自空分压力塔顶部的纯液氮进入压力塔顶部冷凝器作冷源，被蒸发的气氮在冷却器冷却液化后再经减压降温后进入低压塔顶部的冷凝器中作塔的冷源，蒸发氮气出塔经复热后作产品气。
d.液氩在低压塔精馏后，在低压塔顶部排出少量废气，在低压塔下部冷凝器获得精氩液体或精氩气体产品。
7.双级精馏塔附设一只精氩塔的空气分离设备流程，其特征：
a.精氩塔由压力塔和低压塔组成，中间设置一只冷凝蒸发器，在低压塔顶部设置一只冷凝器，由空分压力塔净化原料空气入口处下部所设置的提馏段中部的氩馏份富集区引出一部分氩馏份气体，进入精氩塔的压力塔下部作原料气。
b.原料气在压力塔内精馏分离后，在塔底所获得的富氧液体，仍回入空分压力塔相应部位，在压力塔顶部获得的粗氩液体，经减压降温后进入低压塔中部进行再次精馏。
c.引入来自空分压力塔顶部主冷凝器内的部分液氧进入精氩压力塔项部冷凝器作冷源，被蒸发的气氧出冷凝器后与空分主冷凝器所引出的气氧汇合，复热至常温后出装置作产品气。
b.引入来自空分低压塔顶部冷凝器内的低压纯液氮进入精氩低压塔顶部冷凝器作冷源，被蒸发的气氮出冷凝器后与空分低压塔顶部冷凝器作蒸发的气氮汇合后，复热至常温后出装置作产品气。
e.液氩在低压塔精馏后，在低压塔顶部排出少量废气，在低压塔下部冷凝器获得精氩液体或精氩气体产品。
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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101636627B (zh) * 2007-01-16 2011-09-07 乔治洛德方法研究和开发液化空气有限公司 使用交叉波纹规整填料塔分离气体混合物的分离方法
CN104034124A (zh) * 2014-06-27 2014-09-10 莱芜钢铁集团有限公司 一种空气分离装置与带压排液方法
WO2015014485A3 (de) * 2013-08-02 2015-09-24 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung von druckstickstoff
CN105865148A (zh) * 2016-04-01 2016-08-17 上海启元空分技术发展股份有限公司 一种高效生产高纯氧和高纯氮的方法
CN107062801A (zh) * 2017-06-05 2017-08-18 杭州特盈能源技术发展有限公司 一种窑炉用深冷直送低压富氧制取装置和方法
CN107062802A (zh) * 2017-06-05 2017-08-18 杭州特盈能源技术发展有限公司 一种窑炉用低压富氧制取装置和方法

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101636627B (zh) * 2007-01-16 2011-09-07 乔治洛德方法研究和开发液化空气有限公司 使用交叉波纹规整填料塔分离气体混合物的分离方法
WO2015014485A3 (de) * 2013-08-02 2015-09-24 Linde Aktiengesellschaft Verfahren und vorrichtung zur erzeugung von druckstickstoff
CN104034124A (zh) * 2014-06-27 2014-09-10 莱芜钢铁集团有限公司 一种空气分离装置与带压排液方法
CN105865148A (zh) * 2016-04-01 2016-08-17 上海启元空分技术发展股份有限公司 一种高效生产高纯氧和高纯氮的方法
CN107062801A (zh) * 2017-06-05 2017-08-18 杭州特盈能源技术发展有限公司 一种窑炉用深冷直送低压富氧制取装置和方法
CN107062802A (zh) * 2017-06-05 2017-08-18 杭州特盈能源技术发展有限公司 一种窑炉用低压富氧制取装置和方法

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