CN101464085A - 一种超低压单塔深冷空分工艺 - Google Patents

一种超低压单塔深冷空分工艺 Download PDF

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CN101464085A
CN101464085A CNA2009101108370A CN200910110837A CN101464085A CN 101464085 A CN101464085 A CN 101464085A CN A2009101108370 A CNA2009101108370 A CN A2009101108370A CN 200910110837 A CN200910110837 A CN 200910110837A CN 101464085 A CN101464085 A CN 101464085A
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尤彪
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BEIJING MINGDU HOUDE TECHNOLOGY 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
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    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—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
    • F25J3/04309—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 nitrogen
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a 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
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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

Abstract

本发明公开了一种超低压单塔深冷空分工艺，其工艺过程包括空气或富氧空气的压缩，空气或富氧空气除水、净化、换热，氮气压缩和换热，氮气或空气膨胀制冷，液氮和液空(或富氧液空)制取，超低压单塔精馏制取气氧和气氮等步骤。由于精馏完全在单塔低压力下进行，由于设有氮气压缩机，因此，液氮纯度完全有保证，精馏过程易于进行，阻力小，可采用低液气比，节能、工程造价低、操作调节方便、产品方案灵活、易于和富氧装置形成大型联合制氧机组、从而降低能耗和实现装置大型化，同样制氧量的条件下，可以较大幅度提高氮气产量。

Description

一种超低压单塔深冷空分工艺
技术领域
本发明涉及空气分离工艺技术领域，尤其涉及超低压单塔深冷空分工艺技术领域。
背景技术
氧气和氮气在工业生产上有广泛的用途，大气是氮气和氧气取之不尽的来源，因此工业上氧氮气均通过空气分离的办法制取，其中运用最为广泛的是深冷空气分离方法，目前深冷空气分离法工艺普遍的流程多为全低压双塔精馏分离流程。
其工艺过程包含以下步骤：
a.空气的压缩；
b.空气除水、净化、换热；
c.空气膨胀制冷；
d.液氮和液空的制取；
e.全低压双塔精馏制取气氧和气氮。
具体过程如下：空气压缩至0.58～0.6MPa(压力均指绝对压力，以下同)，经冷却、冷冻除水，纯化器净化，经主换热器和返流气体换热后，小部分经膨胀机涡轮增压膨胀后压力降至0.13～0.15MPa，进上塔精馏，大部分进入下塔制取液氮和液空，液氮和液空经返流气氮过冷后节流进入上塔作为精馏回流液，上塔和下塔之间设置主冷凝器，由上塔液氧冷却下塔顶部的气氮制取液氮同时使液氧汽化，部分液氮过冷后减压进入上塔顶部作为回流液，一部分作为下塔回流液，使空气得到初步分离，从而得到含氧38～40％的液空。气氧和气氮分别从上塔底部和顶部引出，经主换热器和压缩空气换热复热后作为产品引出。
以上现有流程的主要缺点有以下几点：
1、该流程全部的原料空气均需压缩至0.58～0.6MPa，功耗大、能耗高。
2、该流程下塔在0.55～0.58MPa压力下运行，目前多采用筛板塔，由于阻力大，所设塔板数不能太多，为了保证液氮的纯度，只能采用高回流比操作，工作回流比大于最小工作回流比30～50％，液空氧含量仅为38～40％。
3、双塔流程气氮、气氧的纯度既受限于下塔的塔板数和液气比，也受限于上塔的液气比和塔板数，在不设辅塔的情况下难以制取高纯氮，增设辅塔的情况下虽能制取高纯氮(气氮纯度仍受下塔液氮纯度的制约)但需引出大量的污氮，一方面降低氧的提取率，同时又降低了高纯氮的产量。
4、流程复杂，制冷和精馏过程间存在关联藕合关系，由于两过程间相互制约，液体产品数量难以大幅度提高。
发明内容
本发明的目的是提供一种节能、工程造价低、操作调节方便、产品方案灵活、易于大型化的超低压单塔深冷空分工艺。
本发明为达到以上目的所采用的技术方案是：一种超低压单塔深冷空分工艺，其工艺过程包含以下步骤：
a.空气或富氧空气的压缩；
b.空气或富氧空气除水、净化、换热；
c.氮气压缩和换热；
d.氮气或空气膨胀制冷；
e.液氮和液空或富氧液空的制取；
f.超低压单塔精馏制取气氧和气氮。
其工艺过程中的c步骤中设置有氮气压缩机，氮气压缩机将压缩后的氮气冷却，经主换热器换热后，可以是用于膨胀机膨胀制冷，或是通过设置在精馏塔底部冷凝器和液氧换热制取液氮以作为精馏的回流液。
其工艺过程中的a步骤中空气或富氧空气的压缩分为两部分，甲部分空气或富氧空气压缩至绝对压力0.14～0.17MPa，经冷却、冷冻除水，纯化器净化并和返流气在主换热器换热后进入精馏塔分离；乙部分空气或富氧空气压缩至绝对压力0.14～0.55MPa，经冷却、冷冻除水，纯化器净化后，经主换热器和返流气体换热，可以是将乙部分空气通过膨胀机膨胀制冷，膨胀后的乙部分空气或富氧空气和甲部分空气或富氧空气汇合后进入精馏塔精馏；也可以将经压缩、冷却、换热后的空气或富氧空气通过设置在精馏塔底部的冷凝器和液氧换热后制取液空作为精馏塔回流液。
其工艺过程中的f步骤中精馏工步中所用精馏塔是单精馏塔，该单精馏塔绝对压力为0.1～0.15Mpa。
本实用新型的有益效果是：
1.由于空气精馏完全在0.1～0.15MPa的低压力下进行，使精馏过程易于进行，加上可以采用规整填料，阻力小，可以增加塔板数，加上采用氮气压缩制取液氮，液氮纯度完全有保证，(液氮纯度等于气氮纯度，从而使气氮纯度有自提高的趋势)，从而使采用低液气比操作成为可能。
2.由于回流比降低，返流气氮数量的增加，使液空液氮的过冷度更有保证，降低液氮、液空(或富氧液空)的气化率又进一步降低能耗。
3.无论采用氮膨胀还是空气膨胀，精馏过程和制冷过程均不再相互影响，可以灵活的安排液体产品的比例。
4.气氧的纯度可以通过液空制取量来进行调节。气氮的纯度可以通过液氮制取量来进行调节。对于制取高纯氧和高纯氮十分有利。
5.由于设有氮气压缩机，相应增加氮液化配置既可以增加液体产品，也可以为内压缩流程提供补充冷量，有可能使整个流程形成模块化格局，实现设计的标准化。
6.易于和富氧装置形成大型联合制氧机组，从而降低能耗和实现装置大型化。
7.同样制氧量的条件下，可以较大幅度提高氮气产量。
附图说明
下面结合附图和具体实施方式对本发明作进一步详细的说明。其中：
图1是现有典型深冷空分工艺生产过程的流程图；
图2是本发明的第一种实施例的流程图；
图3是本发明的第二种实施例的流程图；
图4是本发明的第三种实施例的流程图；
图5是本发明的第四种实施例的流程图。
附图中的标记编号说明如下：
氧气O2、氮气N2、空气Air、液氮LN、污氮WN、液氧L0、液空LAir、单精馏塔C、上精馏塔C2、下精馏塔C1、主换热器E1、过冷器E2、膨胀机ET、冷凝器K、纯化器、氮气压缩机NP、富氧空气压缩机NP1、氮气压缩机甲NP2、涡轮增压机B、涡轮增压机甲B1、涡轮增压机乙B2、水洗塔AC、纯化器甲MS1、纯化器乙MS2。
具体实施方式
现有典型深冷空分工艺生产过程的流程，为全低压双塔精馏分离流程，如图1所示，空气压缩至0.58～0.6MPa(压力均指绝对压力，以下同)，经水洗塔AC冷却、冷冻除水，经并联的纯化器甲MS1、纯化器乙MS2净化，小部分经并联的涡轮增压机甲B1、涡轮增压机乙B2增压；膨胀机甲ET1、膨胀机乙ET2膨胀后压力降至0.13～0.15MPa，并经主换热器E1和返流气体换热后，进上精馏塔C2精馏，大部分经主换热器E1和返流气体换热后，进入下精馏塔C1制取液氮和液空，液氮和液空经过冷器E2与返流气氮过冷后节流进入上精馏塔C2作为精馏回流液，上精馏塔C2和下精馏塔C1之间设置主冷凝器K，由上精馏塔C2液氧冷却下精馏塔C1顶部的气氮制取液氮同时使液氧汽化，部分液氮经过冷器E2过冷后减压进入上精馏塔C2顶部作为回流液，一部分作为下精馏塔C1回流液，使空气得到初步分离，从而得到含氧38～40％的液空。气氧和气氮分别从上精馏塔C2底部和顶部引出，经主换热器K和压缩空气换热复热后作为产品引出，过冷器E2排出的污氮经主换热器K换热后排出。
本发明的第一种实施例，如图2所示，状态流量为57000m3/h，温度为30℃，含水率为5％的空气分为两个部分，其中一部分状态流量为24500m3/h的空气压缩至0.14～0.55MPa，经冷却、冷冻除水，纯化器净化后，经主换热器E1和返流气体换热，该部分中的标准流量为10000m3/h的空气经涡轮增压机B增压，膨胀机ET膨胀后进入单精馏塔C进行精馏，该单精馏塔C压力为0.1～0.15Mpa，该部分中的标准流量为12450m3/h的空气在单精馏塔C底部的液空冷凝器K冷凝制取液空，同时使液氧蒸发，液空经过过冷器E2和气氮换热后进入单精馏塔C中部作为回流液；另一部分状态流量为32500m3/h的空气压缩至0.14～0.17MPa，经冷却、冷冻除水，纯化器净化后，经主换热器E1和返流气体换热后和膨胀空气汇合进入单精馏塔C精馏，返流的氮气状态流量为52000m3/h，经过过冷器E2与液空、液氮换热后，经主换热器E1和正流压缩气体换热，复热后的氮气，一部分作为产品氮气引出，另一部分标准流量为12000m3/h的氮气经氮气压缩机NP压缩至0.58MPa，经冷却通过主换热器E1与返流气体换热后进入单精馏塔C底部设置的液氮冷凝器K冷凝制取液氮同时使液氧蒸发。液氮经过冷器E2后节流进入单精馏塔C顶部作为回流液。标准流量为10000m3/h的气氧从单精馏塔C底部引出，经主换热器E1换热后，作为产品气引出。
本发明的第二种实施例，如图3所示，状态流量为57000m3/h，温度为30℃，含水率为5％的空气分为两个部分，其中一部分状态流量为11000m3/h的空气压缩至0.14～0.55MPa，经冷却、冷冻除水，纯化器净化后，经主换热器E1和返流气体换热后经涡轮机B增压，膨胀机ET膨胀后进入单精馏塔C，该单精馏塔C压力为0.1～0.15Mpa，其中另一部分标准流量为46000m3/h的空气压缩至0.14～0.17MPa，经冷却冷冻除水、纯化器净化后，进入主换热器E1与返流气换热，换热后的空气和膨胀空气汇合进入单精馏塔C精馏，从单精馏塔C顶部引出流量为63000标准m3/h的气氮经过冷器E2与液氮换热后，进入主换热器E1与正流压缩气体换热，复热后的氮气大部分作为产品氮气引出，其中标准流量为23000m3/h的氮气经氮气压缩机甲NP2压缩至0.58Mpa，经冷却后，通过主换热器E1换热，再进入单精馏塔C底设置的冷凝器K冷凝，同时使液氧气化，液氮经过过冷器E2过冷后节流进入单精馏塔C顶部作为回流液，标准流量为10000m3/h的气氧从单精馏塔C底部引出，经主换热器E1复热后作为产品引出。
本发明的第三种实施例，如图4所示，标准流量为57000m3/h、温度为30℃、含水率为5％的空气压缩至0.14～0.17MPa，经冷却冷冻除水、纯化器净化后，进入主换热器E1与返流气换热后进入单精馏塔C精馏，该单精馏塔C压力为0.1～0.15Mpa，从单精馏塔C顶部引出的标准流量为63000m3/h的氮气经过冷器E2与液氮换热后，经主换热器E1与压缩空气换热，复热后的氮气大部分作为产品氮气引出，其余标准流量为31000m3/h的氮气经氮气压缩机NP压缩至0.58Mpa，经冷却通过主换热器E1与返流气体换热后，分为两个部分，其中一部分标准流量为8000m3/h的氮气经涡轮增压机B增压，膨胀机ET膨胀后，进入主换热器E1复热后，作为产品引出；另一部分标准流量为23000m3/h的氮气进入单精馏塔C底部设置的冷凝器K冷凝制取液氮，同时使液氧气化，液氮经过冷器E2过冷后，节流进入单精馏塔C上部作为回流液，标准流量为10000m3/h的气氧从单精馏塔C底部引出，经主换热E1复热后作为产品引出。
本发明的第四种实施例，如图5所示，标准流量为50000m3/h的富氧空气经冷却冷冻除水、纯化器净化后，分为两个部分，其中一部分标准流量为330000m3/h的富氧空气经富氧空气压缩机NP1压缩至0.14～0.55MPa，经主换热器E1与返流气体换热后，进入单精馏塔C底部设置的冷凝器K冷凝制取富氧液空，同时使液氧蒸发，富氧液空经过冷器E2过冷后，节流进入单精馏塔C中部作为回流液；该单精馏塔C压力为0.1～0.15Mpa，另一部分标准流量为17000m3/h的富氧空气压力为0.14～0.17MPa，经主换热器E1换热后，进入单精馏塔C进行精馏，从单精馏塔C顶部引出的标准流量为32000m3/h的气氮，经过冷器E2与富氧液空、液氮换热后，经主换热器E1与正流气体换热，复热后的气氮其中一部分作为产品引出，其余标准流量为20000m3/h的气氮经氮气压缩机甲NP2压缩至0.58Mpa，经主换热器E1复热后，其中标准流量为8000m3/h的气氮经涡轮增压机B增压，膨胀机ET膨胀后，经主换热器E1复热作为产品引出，标准流量为12000m3/h的气氮进入单精馏塔C底部设置的冷凝器K冷凝制取液氮，同时使液氧蒸发，液氮经过冷器E2过冷后，节流进入单精馏塔C顶部作为回流液，标准流量为30000m3/h的气氧从单精馏塔C底部引出，经主换热E1复热后作为产品引出。
当然，本发明中标出的各流量值、压力值、温度值、含水率值、空气或富氧空气的分流比值均为参考值，实施中适度的变动并不会影响本发明的技术效果，因此，以上数值的适度改变均应是落在本发明的保护范围内。

Claims (4)

1、一种超低压单塔深冷空分工艺，其特征在于：其工艺过程包含以下步骤：
a.空气或富氧空气的压缩；
b.空气或富氧空气除水、净化、换热；
c.氮气压缩和换热；
d.氮气或空气膨胀制冷；
e.液氮和液空或富氧液空的制取；
f.超低压单塔精馏制取气氧和气氮。
2.根据权利要求1所述的一种超低压单塔深冷空分工艺，其特征在于：其工艺过程中的c步骤中设置有氮气压缩机，氮气压缩机将压缩后的氮气冷却，经主换热器换热后，压缩后的氮气可以是用于膨胀机膨胀制冷，或是通过设置在精馏塔底部冷凝器和液氧换热制取液氮以作为精馏的回流液。
3.根据权利要求1所述的一种超低压单塔深冷空分工艺，其特征在于：其工艺过程中的a步骤中空气或富氧空气的压缩分为两部分，甲部分空气或富氧空气压缩至绝对压力0.14～0.17MPa，经冷却、冷冻除水，纯化器净化并和返流气在主换热器换热后进入精馏塔分离；乙部分空气或富氧空气压缩至绝对压力0.14～0.55MPa，经冷却、冷冻除水，纯化器净化后，经主换热器和返流气体换热，可以是将乙部分空气通过膨胀机膨胀制冷，膨胀后的乙部分空气或富氧空气和甲部分空气或富氧空气汇合后进入精馏塔精馏；也可以将经压缩、冷却、换热后的空气或富氧空气通过设置在精馏塔底部的冷凝器和液氧换热后制取液空作为精馏塔回流液。
4.根据权利要求1所述的一种超低压单塔深冷空分工艺，其特征在于：其工艺过程中的f步骤中精馏工步中所用精馏塔是单精馏塔，该单精馏塔绝对压力为0.1～0.15Mpa。
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CN103970168A (zh) * 2014-05-20 2014-08-06 厦门大学 超低压单塔深冷空分过程控制系统
CN105858615A (zh) * 2016-05-05 2016-08-17 珠海辉钰医疗科技有限公司 一种桥式低压风机制氧系统
CN114165989A (zh) * 2021-11-22 2022-03-11 四川空分设备(集团)有限责任公司 制取中压氮气的装置及方法

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US4464188A (en) * 1983-09-27 1984-08-07 Air Products And Chemicals, Inc. Process and apparatus for the separation of air
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CN103970168A (zh) * 2014-05-20 2014-08-06 厦门大学 超低压单塔深冷空分过程控制系统
CN103970168B (zh) * 2014-05-20 2016-02-17 厦门大学 超低压单塔深冷空分过程控制系统
CN105858615A (zh) * 2016-05-05 2016-08-17 珠海辉钰医疗科技有限公司 一种桥式低压风机制氧系统
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