CN101492156B - 低能耗制氮方法和装置 - Google Patents

低能耗制氮方法和装置 Download PDF

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CN101492156B
CN101492156B CN2009100585832A CN200910058583A CN101492156B CN 101492156 B CN101492156 B CN 101492156B CN 2009100585832 A CN2009100585832 A CN 2009100585832A CN 200910058583 A CN200910058583 A CN 200910058583A CN 101492156 B CN101492156 B CN 101492156B
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nitrogen
heat exchanger
air
oxygen
liquid
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CN101492156A (zh
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黄震宇
李传明
杨斌
刘厚荣
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Sichuan Air Separation Plant (group) Co Ltd
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    • 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
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    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
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    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
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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
    • 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
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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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas

Abstract

本发明涉及低能耗制氮方法和装置，空气冷却后在精馏塔顶获得氮气，一部分被冷凝为液氮，其一部分作为产品液氮，其余作为回流液返回塔顶部；另一部分氮气进入换热器复热到常温，经膨胀机的增压端增压送入用户氮气输送管网；塔底获得富氧液空，进入换热器被冷流体过冷，节流再入冷凝蒸发器作为冷源与氮气进行换热，蒸发的富氧气进入换热器被复热后再入膨胀机膨胀制冷，膨胀后的低压富氧气体进入换热器复热引出。本发明通过富氧气膨胀输出的功增压氮气，降低了压缩机排压从而降低了能耗，以及液空被低压富氧气、氮气和压力富氧气等各种冷流体换热过冷，降低空气的含湿量提高提取率，降低能耗15~23％，水耗14~22％，经济效益十分可观。

Description

低能耗制氮方法和装置
技术领域
本发明涉及一种大幅度降低能耗制氮方法和装置。
背景技术
随着新兴光电产业和特殊石化行业等的飞速发展，对氮气产品的需求量越来越大，制取氮气的空分设备是耗能大户，由于长期运行，如何能有效降低能耗至关重要。氮气压力较高，富氧气量较大，充分膨胀利用则输出功率可观，目前一般的做法是部分膨胀，其余节流，膨胀机输出的功增压原料空气或采用风机制动放空；液空不过冷或仅与部分流体简单换热过冷。采用这些方法和流程组织，空分设备的能耗无法满足用户的要求。
发明内容
本发明要解决的技术问题是提供一种工艺优化、成本低、节能降耗的制氮方法和装置。
为解决上述技术问题，本发明的制氮方法包括如下步骤：
a)压缩并净化的空气引入换热器进行低温冷却；
b)冷却后的空气送入精馏塔，在精馏塔从下而上在塔板或填料上与自上而下的液体进行传热传质，在塔顶获得氮气；
c)从精馏塔顶出来的一部分氮气进入冷凝蒸发器被冷凝成液氮，所述的液氮一部分作为产品液氮被引出，其余部分液氮作为回流液返回精馏塔；从塔顶出来的另一部分氮气送入换热器复热到常温，然后进入膨胀机的增压端增压后进入用户氮气管网；
d)从精馏塔底引出的富氧液空，进入所述换热器进行过冷换热，节流后进入所述冷凝蒸发器作为冷源，富氧液空在冷凝蒸发器内蒸发后产生的压力富氧气送入上述换热器被复热后再送入上述膨胀机膨胀制冷，膨胀后产生的低压富氧气进入换热器被复热至常温被排出，其膨胀输出的功用于驱动膨胀机增压端增压氮气。
为了解决以上技术问题，本发明的制氮装置包括：
a)增压透平膨胀机，膨胀端与增压端通过轴连接，膨胀端膨胀输出的功可驱动增压端增压；
b)冷凝蒸发器；
c)换热器，压缩并净化的空气引入换热器进行低温冷却；
d)精馏塔，低温冷却后的空气送入精馏塔分离；塔底获得富氧液空，塔顶获得氮气；
塔顶获得的一部分氮气通过管道送入所述换热器，换热器通过管道依次与上述膨胀机的增压端连接；塔顶获得的另一部分氮气通过管道送入上述冷凝蒸发器冷凝后，其中一部分液氮通过管道引出作为产品，其他部分液氮作为回流液返回所述精馏塔；
塔底的富氧液空送入上述换热器进行热交换后通过管道进入冷凝蒸发器作为冷源，富氧液空在冷凝蒸发器内蒸发后产生的压力富氧气通过管道送入上述换热器，被复热后再通过管道送入上述膨胀机，其膨胀输出的功用于驱动膨胀机增压端增压氮气；膨胀后的低压富氧气通过管道进入换热器被复热至常温被排出。
本发明利用富氧液空在冷凝蒸发器内蒸发产生的压力富氧气在膨胀机膨胀输出的功增压氮气，充分有效利用了能量，压缩机排压和精馏压力降低，降低了原料气的压力，利于精馏，并大幅度降低能耗。其次将富氧液空与压力富氧气、低压富氧气和氮气等冷流体换热过冷，返流气体将引入的压缩净化后的空气低温冷却；可以充分回收冷量，特别是降低了液空节流汽化率，增大精馏塔回流比；降低了入塔空气的含湿量，参与精馏的空气比率增大；提高了膨胀机入口温度，高温高焓降，膨胀机制冷量输出功增大，液空充分过冷吸收冷量，含湿量降到最低，相当于增加了精馏气量，提高了提取率。避免了大量膨胀导致空气含湿量增加的问题，同时增大了液氮的产量，提高了输出产品的经济价值。采用本发明，具有流程组织优化，设备投入成本低，能耗降低显著的特点。
附图说明
图示为本发明的制氮工艺流程和装置。
图中标记：
ET增压膨胀机
C1精馏塔
K1冷凝蒸发器
E1换热器
具体实施方式
下面结合附图和具体实施方式对本发明作进一步详细说明。但不应将此理解为本发明的上述主题的范围仅限于下述实施例。
如图所示，本发明的制氮工艺流程如下：
a)压缩并净化的空气引入换热器E1，通过管道被换热器内的低压富氧气、氮气和压力富氧气等返流气体冷却到接近液化温度；
b)冷却后的空气送入精馏塔C1，在精馏塔从下而上在塔板或填料上与自上而下的液体进行传热传质，塔内由于气液直接接触介质组成沸点不同形成精馏。在塔顶获得氮气；塔底获得富氧液空；
c)从精馏塔顶出来的一部分氮气进入冷凝蒸发器K1被冷凝成液氮，其中一部分液氮作为产品液氮被引出，其余作为回流液返回精馏塔；从塔顶出来的另一部分氮气送入换热器E1复热到常温，然后进入增压膨胀机ET的增压端增压后进入用户氮气管网；
d)从精馏塔底引出的富氧液空，进入换热器E1与低压富氧气、氮气和压力富氧气过冷，节流后进入冷凝蒸发器作为冷源与精馏塔顶出来的氮气进行换热，被蒸发后产生的压力富氧气进入换热器被复热到一定温度，再送入增压膨胀机的膨胀端膨胀制冷；膨胀后的低压富氧气进入换热器被复热至常温被排出。
和现有工艺比较，采用本发明装置和工艺流程，只需要对流程组织进行优化，换热器布置流道略复杂，换热器长度略增加，液空管路略长；用于增压的透平膨胀机及其辅助仪控系统等等费用略增加，但压缩机费用降低，投入成本非常低廉，却可将中大型制氮及其衍生系列装置(如附带部分氧气或液氧)的能耗降低15~23％以上，同时可节约水耗14~22％。例如一套5000NM3/H压力0.9MPaG电子行业典型制氮装置，电耗可降低~373KW(~21.6％)，节水~21％，电费年节约373X0.5X8500＝1,585,250元，按一套装置运行15年计算，节电经济效益为23,778,750元；也即节约资金相当于全部装置投资和管理费用。而本发明装置增加投资的费用回收周期仅需4～8个月，具有经济效益最大化和增加投资最小化的特点，国家提倡节能降排，本发明装置效果显著，意义重大，非常值得推广。全国制氮装置近百套，若采用本发明，每年可节约数亿元电费和大量水资源。
典型制氮装置能耗对比
  流程组织形式   本发明   常规制氮
  产品氮气产量Nm<sup>3</sup>/h   5000   5000
  产品氮气压力MPa.G   0.9   0.9
  产品液氮产量Nm<sup>3</sup>/h   441   441
  空压机排压bara   8.5   11
  空压机排气量Nm<sup>3</sup>/h   13000   14700
  空压机功率KW   1351KW   1726KW
  纯化系统再生气量Nm3/h(15℃吸附)   3419   3463
  加热时间MIN   57   52
  再生平均功率KW(170℃再生)   48   44
  循环水量T/h6℃温升(压缩机)   189   241
  预冷消耗冷量KW   168   176
  预冷消耗冷量折合电耗KW(制冷系数3.8)   44   46
  总功率KW   1443   1816
  节约电耗KW   373   0
  节电   21.6％   0
  节约水   21％
注：预冷、纯化再生为制氮装置预处理。
需要说明的是：虽然上述实施例已经详细描述了本发明的结构，但本发明并不限于上述实施例，凡是本领域技术人员从上述实施例中不经过创造性劳动就可以想到的替换结构和工艺流程，均属于本发明的保护范围。

Claims (2)

1.一种低能耗制氮方法，其特征在于，包括如下步骤：
a)压缩并净化的空气引入换热器进行低温冷却；
b)冷却后的空气送入精馏塔，在精馏塔从下而上在塔板或填料上与自上而下的液体进行传热传质，在塔顶获得氮气；
c)从精馏塔顶出来的一部分氮气进入冷凝蒸发器被冷凝成液氮，所述的液氮一部分作为产品液氮被引出，其余液氮作为回流液返回精馏塔；从塔顶出来的另一部分氮气送入换热器复热到常温，然后进入膨胀机的增压端增压后进入用户氮气管网；
d)从精馏塔底引出的富氧液空，进入所述换热器进行过冷换热，节流后进入所述冷凝蒸发器作为冷源，富氧液空在冷凝蒸发器内蒸发后产生的压力富氧气送入上述换热器被复热后再送入上述膨胀机膨胀制冷，膨胀后产生的低压富氧气进入换热器被复热至常温被排出，其膨胀输出的功用于驱动膨胀机增压端增压氮气。
2.一种低能耗制氮装置，其特征在于：包括如下装置，
a)增压透平膨胀机，膨胀端与增压端通过轴连接，膨胀端膨胀输出的功可驱动增压端增压；
b)冷凝蒸发器；
c)换热器，压缩并净化的空气引入换热器进行低温冷却；
d)精馏塔，低温冷却后的空气送入精馏塔分离；塔底获得富氧液空，塔顶获得氮气；
塔顶获得的一部分氮气通过管道送入所述换热器，换热器通过管道依次与上述膨胀机的增压端连接；塔顶获得的另一部分氮气通过管道送入上述冷凝蒸发器冷凝后，其中一部分液氮通过管道引出作为产品，其他部分液氮通过回流管道作为回流液返回所述精馏塔；
塔底的富氧液空送入上述换热器进行热交换后通过管道进入冷凝蒸发器作为冷源，富氧液空在冷凝蒸发器内蒸发后产生的压力富氧气通过管道送入上述换热器，被复热后再通过管道送入上述膨胀机，其膨胀输出的功用于驱动膨胀机增压端增压氮气；膨胀后的低压富氧气通过管道进入换热器被复热至常温被排出。
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