CN101915495B - 利用液化天然气冷能的全液体空气分离装置及方法 - Google Patents

利用液化天然气冷能的全液体空气分离装置及方法 Download PDF

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CN101915495B
CN101915495B CN2010102623634A CN201010262363A CN101915495B CN 101915495 B CN101915495 B CN 101915495B CN 2010102623634 A CN2010102623634 A CN 2010102623634A CN 201010262363 A CN201010262363 A CN 201010262363A CN 101915495 B CN101915495 B CN 101915495B
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nitrogen
liquid
air
heat exchanger
pipeline
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CN101915495A (zh
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刘景武
郑小平
马源
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KAIFENG AIR SEPARATION GROUP CO Ltd
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    • 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
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Abstract

本发明涉及一种利用液化天然气冷能的全液体空气分离装置及方法，包括包括：自洁式空气过滤器AF、空气压缩机TC1、空气冷却器E5、纯化***、主换热器E2、液化器E7、下塔C1、与下塔C1通过管道并经过过冷器E3后相连通的上塔C2、第一冷凝蒸发器K1、氮气循环***、以及氩气分馏***，所述的下塔C1上设置有污液氮、贫液空抽口，过冷器E3上设置有污液氮通道和贫液空通道，上塔C2上设置有污液氮、贫液空进口，污液氮通道通过过冷器E3分别与上塔C2和下塔C1相连通，贫液空通道通过过冷器E3分别与上塔C2和下塔C1相连通；本发明冷量利用率高、节能环保、工作效率高、安全系数高。

Description

利用液化天然气冷能的全液体空气分离装置及方法
技术领域
本发明涉及空气分离装置，具体涉及一种利用液化天然气冷能的全液体空气分离装置及方法。
背景技术
空气分离设备就是将空气液化、精馏、最终分离成为氧、氮和其他有用气体的气体分离设备，简称空分设备。空气曾被称为“永久气体”到19世纪末，人们发现在深低温下空气也能液化，并因氧、氮沸点不同，可以从液化空气中分离出氧气和氮气。第一台商品化的制氧机于1903年制成，它最初只是用于金属的气焊和切割。30年代末，氮肥工业需要氮气，制氧机发展到能同时生产氧气和氮气，改称空气分离设备。
天然气是一种优质能源，具有热值高、洁净、燃烧污染小等特点，其主要成份是甲烷，为了便于运输将其液化液化温度一般在-150℃～-161℃)，成为液化天然气LNG)，输送到目的地后为了利用又需将其汽化，汽化时会产生大量的冷量，0.1Mpa下的LNG从-161℃复热到27℃时所释放的冷能约为950KJ/kg，8.0Mpa下的NG从-161℃复热到27℃时所释放的冷能约为830KJ/kg，LNG蕴藏有巨大的高品质冷能，如果不回收利用将是极大的浪费。目前LNG冷能利用的方式有冷能发电、低温粉碎旧轮胎、生产液氧、液氮、液氩的全液体空分装置。根据低温冷量尽可能低温利用的原理，全液体空分装置是LNG冷能利用最有效最合理的一种利用方式。
全液体空分装置生产的液氧、液氮、液氩产品广泛应用于冶金、石化、机械、化肥、玻璃、军工、食品、医疗等领域，但传统的常规空分能耗大，生产1Nm3液体产品需1.05-1.25kwh的能耗，利用LNG冷能的空分装置生产1Nm3液体产品能耗降低50％以上。
发明内容
针对现有技术的不足，本发明提供一种冷量利用率高、节能环保、工作效率高、安全系数高的利用液化天然气冷能的全液体空气分离装置及方法。
本发明的技术方案是这样实现的：一种利用液态天然气冷能的全液体空气分离装置，包括：自洁式空气过滤器AF、与自洁式空气过滤器AF相连通的空气压缩机TC1、与空气压缩机TC1相连通的空气冷却器E5、与空气冷却器E5相连通的纯化***、通过第一原料空气管道与纯化***相连接的主换热器E2、与第一原料空气管道相连通的第二原料空气管道、与第二原料空气管道相连通的下塔C1、与下塔C1通过管道并经过过冷器E3后相连通的上塔C2、位于上塔C2底部的第一冷凝蒸发器K1、与下塔C1相连通的氮气循环***、以及与上塔C2相连通的氩气分馏***，所述的下塔C1上设置有污液氮、贫液空抽口，过冷器E3上设置有污液氮通道和贫液空通道，上塔C2上设置有污液氮、贫液空进口，污液氮通道通过过冷器E3分别与上塔C2和下塔C1相连通，贫液空通道通过过冷器E3分别与上塔C2和下塔C1相连通。
所述的氮气循环***包括高压换热器E1、输送液态天然气到高压换热器E1用于回收液态天然气冷量的液态天然气管道、与下塔C1通过第一管道相连通的低压循环氮压机TC2、与低压循环氮压机TC2相连通的中压循环氮压机TC3、与低压循环氮压机TC2和中压循环氮压机TC3通过第五管道相连通的第一气液分离器SV1、通过第六管道与第一气液分离器SV1相连通的第二气液分离器SV2、通过第二管道与第一气液分离器SV1相连通的液化器E7，其中第一气液分离器SV1通过第七管道与低压循环氮压机TC2相连通，第五管道上设置有与中压循环氮压机TC3相连通的第八管道，液化器E7又分别通过第三管道以及第四管道与低压循环氮压机TC2相连通。
所述的纯化***通过第一原料空气管道与主换热器E2相连接，第一原料空气管道穿过主换热器E2后与液化器E7相连接，液化器E7通过液空管道与下塔C1相连接。
所述的液态天然气管道26中的天然气的压力为0.2Mpa-10.0Mpa。
一种利用液化天然气冷能的全液体空气分离方法，其方法如下：
1)原料空气经过自洁式空气过滤器AF滤掉灰尘杂质后，进入空气压缩机TC1压缩至0.52Mpa，被冷媒乙二醇水溶液或氟里昂降温到2℃-10℃，然后进入纯化***除去空气中的水份、二氧化碳等杂质，净化后的原料空气去主换热器E2换热，被冷却到-167℃至-170℃，一部分原料空气经第二原料空气管道进入下塔C1；另一部分原料空气经液化器E7液化为液空并经液空管道进入下塔C1，在下塔C1进行热质交换、冷凝蒸发，依次获得氮气、液氮、污液氮、贫液空、富氧液空；
2)所述的1)中的富氧液空经过冷器E3过冷后节流去上塔C2进一步精馏，所述的1)中下塔C1顶部得到的氮气去冷凝蒸发器K1，冷凝成液氮，一部分液氮作为下塔的回流液，另一部分液氮经过冷器E3过冷后去上塔C2进一步精馏，所述的1)中下塔C1得到的污液氮、贫液空分别通过污液氮通道、贫液空通道经过冷器E3过冷后去上塔C2参加进一步精馏；
气氮在冷凝蒸发器K1中被冷凝为液氮的同时，1)中上塔C2中的液氧被蒸发作为上塔C2的上升气，与回流液液氮、富氧液空在填料间传热、传质，氧、氮分离，上塔C2底部得到高纯度的液氧输出冷箱I，上塔C2中部得到体积比为8％-12％氩馏份送入制氩***，制取精氩并输出冷箱I，上塔C2顶部的氮气经过冷器E3、主换热器E2复热后出冷箱I；
3)将1)、2)中下塔C1顶部得到的氮气抽出一部分经第一管道与输出液化器E7中汽化的一部分氮气的第三管道合并后去主换热器E2，与第一原料空气管道换热升温后出冷箱I，然后去冷箱II，在高压换热器E1中被液态天然气冷却到-120℃至-126℃后抽出，送入低压循环氮压机TC2；液化器E7中汽化的另一部分氮气通过第四管道经高压换热器E1升温到-120℃至-126℃后，送入低压循环氮压机TC2，第一气液分离器SV1分离出的氮气也经高压换热器E1升温到-120℃-126℃后抽出，送入低压循环氮压机TC2，经低压循环氮压机TC2增压后返回高压换热器E1再次冷却到-120℃至-126℃后抽出去中压循环氮压机TC3，增压后返回换热器E1，回收液化天然气的冷量，液化为液氮，被液化的液氮一部分节流后经换热器E1升温到-120℃至-126℃后抽出去中压循环氮压机TC3，剩余液氮进第一气液分离器SV1，分离的液氮一部分经第二管道去液化器E7液化空气，自身蒸发为氮气，另一部分液氮去第二气液分离器SV2，分离后的液体作为产品送出，气体经换热器E1复热出冷箱II；
4)所述的3)中的液态天然气管道中的液态天然气在高压换热器E1中被复热，从高压换热器E1中部的液态天然气管道中抽出一部分天然气去换热器E4冷却乙二醇水溶液或氟利昂，剩余部分从高压换热器E1末端抽出与经换热器E4复热后的天然气合并后，最终得到2℃以上的天热气，被冷却的冷媒去空压机中间冷却器E6和末级冷却器E5冷却空气压缩机TC1的压缩空气到到2℃-10℃，提高空气压缩机TC1的效率，降低空气压缩机TC1能耗。
所述的3)中下塔C1顶部抽出一部分氮气经第一管道与输出液化器E7中汽化的一部分氮气的第三管道合并后去主换热器E2，与第一原料空气管道换热升温后出冷箱I，然后去冷箱II，在高压换热器E1中被液态天然气管道冷却到-120℃-126℃后抽出，送入低压氮压机TC2；液化器E7中汽化的另一部分氮气通过第四管道经高压换热器E1升温到-120℃-126℃后，送入低压氮压机TC2，第一气液分离器SV1分离出的氮气通过第七管道也经高压换热器E1升温到-120℃-126℃后抽出，送入低压氮压机TC2，经低温低压循环氮压机TC2增压后返回高压换热器E1冷却，再次冷却到-120℃-126℃后抽出去中压循环氮压机TC3，增压后返回换热器E1，回收液态天然气的冷量，液化为液氮，被液化的液氮一部分经第八管道节流后经换热器E1升温到-120℃-126℃后抽出去中压循环氮压机TC3，剩余液氮通过第五管道进第一气液分离器SV1，分离的液氮一部分经第二管道去液化器E7液化空气，自身蒸发为氮气，另一部分液氮经第六管道去第二气液分离器SV2，液体经液氮输出管道作为产品送出，气体通过第九管道经换热器E1复热出冷箱II。
本发明具有如下的积极效果：本发明通过下塔抽污液氮、贫液空，使空分装置不因部分原料空气的液化而降低提取率；通过循环氮气在高压换热器中液化将LNG的低温冷量回收，乙二醇水溶液(或氟利昂)将高温冷量回收，LNG冷能分阶段利用，与传统的全液体空分装置相比可大幅度降低电耗和水耗；液氮通过液化器将空气液化将冷量传递给分馏塔***，杜绝了甲烷向分馏***的泄露，使分离装置安全性高；LNG在高压换热器中逐步升温气化，将低温冷量转移给氮气，但并没有复热至常温，可以通过合适的冷媒将其高温冷量回收用于空气压缩机的中间冷却和末级冷却，提高空压机机的效率，节能降耗。
附图说明
图1为本发明的结构示意图。
具体实施方式
如图1所示，一种利用液态天然气冷能的全液体空气分离装置，包括：自洁式空气过滤器AF、与自洁式空气过滤器AF相连通的空气压缩机TC1、与空气压缩机TC1相连通的空气冷却器E5、与空气冷却器E5相连通的纯化***、通过第一原料空气管道1与纯化***相连接的主换热器E2、与第一原料空气管道1相连通的第二原料空气管道2、与第二原料空气管道2相连通的下塔C1、与下塔C1通过管道并经过过冷器E3后相连通的上塔C2、位于上塔C2底部的第一冷凝蒸发器K1、与下塔C1相连通的氮气循环***、以及与上塔C2相连通的氩气分馏***，所述的下塔C1上设置有污液氮、贫液空抽口，过冷器E3上设置有污液氮通道6和贫液空通道7，上塔C2上设置有污液氮、贫液空进口，污液氮通道6通过管道分别与上塔C2和下塔C1相连通，贫液空通道7通过管道分别与上塔C2和下塔C1相连通。
所述的氮气循环***包括高压换热器E1、输送液态天然气到高压换热器E1用于回收液态天然气冷量的液态天然气管道26、与下塔C1通过第一管道13相连通的低压循环氮压机TC2、与低压循环氮压机TC2相连通的中压循环氮压机TC3、与低压循环氮压机TC2和中压循环氮压机TC3通过第五管道17相连通的第一气液分离器SV1、通过第六管道20与第一气液分离器SV1相连通的第二气液分离器SV2、通过第二管道19与第一气液分离器SV1相连通的液化器E7，其中第一气液分离器SV1通过第七管道18与低压循环氮压机TC2相连通，第五管道17上设置有与中压循环氮压机TC3相连通的第八管道16，液化器E7又分别通过第三管道14以及第四管道15与低压循环氮压机TC2相连通。
所述的纯化***通过第一原料空气管道1与主换热器E2相连接，第一原料空气管道1穿过主换热器E2后与液化器E7相连接，液化器E7通过液空管道3与下塔C1相连接。
所述的液态天然气管道26中的天然气的压力为0.2Mpa-10.0Mpa。
一种利用液化天然气冷能的全液体空气分离方法，其方法如下：
1)原料空气经过自洁式空气过滤器AF滤掉灰尘杂质后，进入空气压缩机TC1压缩至0.52Mpa，被冷媒乙二醇水溶液(或氟里昂)降温到2℃-10℃，然后进入纯化***除去空气中的水份、二氧化碳等杂质，净化后的原料空气去主换热器E2换热，被冷却到-167℃至-170℃，一部分原料空气经第二原料空气管道2进入下塔C1；另一部分原料空气经液化器E7液化为液空并经液空管道3进入下塔C1，在下塔C1进行热质交换、冷凝蒸发，依次获得氮气、液氮、污液氮、贫液空、富氧液空；
2)所述的1)中的富氧液空经过冷器E3过冷后节流去上塔C2进一步精馏，所述的1)中下塔C1顶部得到的氮气去冷凝蒸发器K1，冷凝成液氮，一部分液氮作为下塔的回流液，另一部分液氮经过冷器E3过冷后去上塔C2进一步精馏，所述的1)中下塔C1得到的污液氮、贫液空分别通过污液氮通道6、贫液空通道7经过冷器E3过冷后去上塔C2参加进一步精馏；
气氮在冷凝蒸发器K1中被冷凝为液氮的同时，1)中上塔C2中的液氧被蒸发作为上塔C2的上升气，与回流液液氮、富氧液空在填料间传热、传质，氧、氮分离，上塔C2底部得到高纯度的液氧输出冷箱I，上塔C2中部得到体积比为8％-12％氩馏份送入制氩***，制取精氩并输出冷箱I，上塔C2顶部的氮气经过冷器E3、主换热器E2复热后出冷箱I；
3)将1)、2)中下塔C1顶部得到的氮气抽出一部分经第一管道13与输出液化器E7中汽化的一部分氮气的第三管道14合并后去主换热器E2，与第一原料空气管道1)换热升温后出冷箱I，然后去冷箱II，在高压换热器E1中被液态天然气管道26冷却到-120℃-126℃后抽出，送入低压氮压机TC2；液化器E7中汽化的另一部分氮气通过第四管道15经高压换热器E1升温到-120℃-126℃后，送入低压氮压机TC2，第一气液分离器SV1分离出的氮气通过第七管道18也经高压换热器E1升温到-120℃-126℃后抽出，送入低压氮压机TC2，经低温低压循环氮压机TC2增压后返回高压换热器E1冷却，再次冷却到-120℃-126℃后抽出去中压循环氮压机TC3，增压后返回换热器E1，回收液态天然气的冷量，液化为液氮，被液化的液氮一部分经第八管道16节流后经换热器E1升温到-120℃-126℃后抽出去中压循环氮压机TC3，剩余液氮通过第五管道17进第一气液分离器SV1，分离的液氮一部分经第二管道19去液化器E7液化空气，自身蒸发为氮气，另一部分液氮经第六管道20去第二气液分离器SV2，液体经液氮输出管道21作为产品送出，气体通过第九管道22经换热器E1复热出冷箱II。
4)所述的3)中的液态天然气管道26中的液态天然气在高压换热器E1中被复热，从高压换热器E1中部的液态天然气管道26中抽出一部分天然气经天然气分支管道23去换热器E4冷却乙二醇水溶液(或氟利昂)，剩余部分从高压换热器E1末端抽出与经换热器E4复热后的天然气经合并后，即与天然气分支管道23合并后，最终得到2℃以上的天热气，被冷却的冷媒通过冷媒输送管道25去空气压机中间冷却器E6和末级冷却器E5冷却空气压缩机TC1的压缩空气到到2℃-10℃，提高空气压缩机TC1的效率，降低空气压缩机TC1能耗。
本发明利用循环氮气通过换热器回收利用LNG冷量，又将空气液化将冷量传递给空分***，通过合适的冷媒将冷量传递给空气压缩***。利用LNG的冷能生产液氧、液氮、液氩，且大幅度降低电耗50％以上、水耗90％以上。通过原料空气传递冷量，避免甲烷往分离***的泄露，安全性高。通过下塔抽取污液氮、贫液空，增加上塔回流比，使空分装置不因原料空气的液化而降低提取率。
本发明并不局限于上述的具体实施方式，上述的具体实施方式仅仅是示意性的，并不是限制性的，本领域的普通技术人员在本发明的启示下，在不脱离本发明宗旨和权利要求所保护的范围情况下，还可以作出很多形式，这些均属于本发明的保护范围之内。

Claims (2)

1.一种利用液化天然气冷能的全液体空气分离方法，其特征在于，其方法如下：
1)原料空气经过自洁式空气过滤器AF滤掉灰尘杂质后，进入空气压缩机TC1压缩至0.52Mpa，被冷媒乙二醇水溶液或氟里昂降温到2℃-10℃，然后进入纯化***除去空气中的水份、二氧化碳杂质，净化后的原料空气去主换热器E2换热，被冷却到-167℃至-170℃，一部分原料空气经第二原料空气管道(2)进入下塔C1；另一部分原料空气经液化器E7液化为液空并经液空管道(3)进入下塔C1，在下塔C1进行热质交换、冷凝蒸发，依次获得氮气、液氮、污液氮、贫液空、富氧液空；
2)所述的1)中的富氧液空经过冷器E3过冷后节流去上塔C2进一步精馏，所述的1)中下塔C1顶部得到的氮气去冷凝蒸发器K1，冷凝成液氮，一部分液氮作为下塔的回流液，另一部分液氮经过冷器E3过冷后去上塔C2进一步精馏，所述的1)中下塔C1得到的污液氮、贫液空分别通过污液氮通道(6)、贫液空通道(7)经过冷器E3过冷后去上塔C2参加进一步精馏；
氮气在冷凝蒸发器K1中被冷凝为液氮的同时，1)中上塔C2中的液氧被蒸发作为上塔C2的上升气，与回流液、富氧液空在填料间传热、传质，氧、氮分离，上塔C2底部得到高纯度的液氧输出冷箱I，上塔C2中部得到体积比为8％-12％氩馏份送入制氩***，制取精氩并输出冷箱I，上塔C2顶部的氮气经过冷器E3、主换热器E2复热后出冷箱I；
3)将1)、2)中下塔C1顶部得到的氮气抽出一部分经第一管道(13)与输出液化器E7中汽化的一部分氮气的第三管道(14)合并后去主换热器E2，与第一原料空气管道(1)换热升温后出冷箱I，然后去冷箱II，在高压换热器E1中被液态天然气(26)冷却到-120℃至-126℃后抽出，送入低压循环氮压机TC2；液化器E7中汽化的另一部分氮气通过第四管道(15)经高压换热器E1升温到-120℃至-126℃后，送入低压循环氮压机TC2，第一气液分离器SV1分离出的氮气也经高压换热器E1升温到-120℃-126℃后抽出，送入低压循环氮压机TC2，经低压循环氮压机TC2增压后返回高压换热器E1再次冷却到-120℃至-126℃后抽出去中压循环氮压机TC3，增压后返回换热器E1，回收液化天然气的冷量，液化为液氮，被液化的液氮一部分节流后经换热器E1升温到-120℃至-126℃后抽出去中压循环氮压机TC3，剩余液氮进第一气液分离器SV1，分离的液氮一部分经第二管道(19)去液化器E7液化空气，自身蒸发为氮气，另一部分液氮去第二气液分离器SV2，分离后的液体作为产品送出，气体经换热器E1复热出冷箱II；
4)所述的3)中的液态天然气管道(26)中的液态天然气在高压换热器E1中被复热，从高压换热器E1中部的液态天然气管道(26)中抽出一部分天然气去换热器E4冷却乙二醇水溶液或氟利昂，剩余部分从高压换热器E1末端抽出与经换热器E4复热后的天然气合并后，最终得到2℃以上的天然气，被冷却的冷媒去空压机中间冷却器E6和末级冷却器E5，冷却空气压缩机TC1的压缩空气到到2℃-10℃，提高空气压缩机TC1的效率，降低空气压缩机TC1能耗。
2.根据权利要求1所述的利用液化天然气冷能的全液体空气分离方法，其特征在于：所述的3)中下塔C1顶部抽出一部分氮气经第一管道(13)与输出液化器E7中汽化的一部分氮气的第三管道(14)合并后去主换热器E2，与第一原料空气管道(1)换热升温后出冷箱I，然后去冷箱II，在高压换热器E1中被液态天然气管道(26)冷却到-120℃-126℃后抽出，送入低压氮压机TC2；液化器E7中汽化的另一部分氮气通过第四管道(15)经高压换热器E1升温到-120℃-126℃后，送入低压氮压机TC2，第一气液分离器SV1分离出的氮气通过第七管道(18)也经高压换热器E1升温到-120℃-126℃后抽出，送入低压氮压机TC2，经低温低压循环氮压机TC2增压后返回高压换热器E1冷却，再次冷却到-120℃-126℃后抽出去中压循环氮压机TC3，增压后返回换热器E1，回收液态天然气的冷量，液化为液氮，被液化的液氮一部分经第八管道(16)节流后经换热器E1升温到-120℃-126℃后抽出去中压循环氮压机TC3，剩余液氮通过第五管道(17)进第一气液分离器SV1，分离的液氮一部分经第二管道(19)去液化器E7液化空气，自身蒸发为氮气，另一部分液氮经第六管道(20)去第二气液分离器SV2，液体经液氮输出管道(21)作为产品送出，气体通过第九管道(22)经换热器E1复热出冷箱II。
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