CN210625120U - 一种HyCO深冷分离装置节能优化系统 - Google Patents

一种HyCO深冷分离装置节能优化系统 Download PDF

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CN210625120U
CN210625120U CN201921419032.XU CN201921419032U CN210625120U CN 210625120 U CN210625120 U CN 210625120U CN 201921419032 U CN201921419032 U CN 201921419032U CN 210625120 U CN210625120 U CN 210625120U
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heat exchanger
tower
denitrification
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章有虎
李元海
杨巧玉
李斌
乔玉珍
刘苗苗
朱明明
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Hangzhou Zhongtai Cryogenic Technology Corp
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Abstract

本实用新型公开了一种HyCO深冷分离装置节能优化系统，属于化工工艺领域。HyCO深冷分离装置包括CO压缩机、脱氮塔顶冷凝器、脱氮塔、脱氮塔底工艺液体节流阀、脱甲烷塔、第二换热器、循环CO节流阀、汽提塔底至脱氮塔节流阀、富氢气闪蒸罐、富氢气闪蒸罐至汽提塔工艺液体节流阀、汽提塔、第一换热器、洗涤液节流阀；本装置工艺流程在工艺液体出脱氮塔后对其进行节流并送至脱氮塔顶部，作为脱氮塔顶部冷源去脱氮塔顶冷凝器，减小了装置对循环介质的需求，从而降低了装置能耗。工艺介质在做冷源的同时自身被汽化后送至脱甲烷塔底部，减小了脱甲烷塔底部再沸器对循环介质的需求，减小了装置能耗。

Description

一种HyCO深冷分离装置节能优化系统
技术领域
本实用新型涉及一种HyCO深冷分离装置节能优化系统，特别是利用工艺液体节流处理后作为脱氮塔顶冷源的优化系统。
背景技术
HyCO主要是氢气与一氧化碳的混合气。HyCO分离装置主要是根据不同物质的沸点不同而使不同的物质进行分离，一般的使用一个分离罐、两塔分离，一塔主要去除溶解在液态CO中的H2，二塔去除CH4。采用两塔分离，气体产品中的CO纯度不高，尤其是当原料中N2的组分较多时，CO产品纯度下降严重，导致产品的不合格。
一种节约冷火炬吹扫氮气的HyCO系统，包括液氮罐、合成气分离装置及火炬，液氮罐底部设有循环管道，管道出口端与火炬管线连接，将液态放空至火炬中，合成气分离装置将低温液相物质汽化，经出口管道导入到火炬中燃烧。由于HyCO深冷分离装置存在大量低温液相物质，故需要一个火炬来排放大量的低温液体，首先需要汽化然后再将气态排入至火炬燃烧，由于进火炬前可能存在末端的气态不容易进入火炬系统，为了确保工艺安全，设计了吹扫氮气来保证进火炬前管线能够全部进入火炬燃烧。
通常HyCO深冷分离装置采用三塔工艺流程时一般依次脱氢、脱氮和脱甲烷顺序，此过程中采用流程是将经过第一换热器、第二换热器的部分冷凝工艺介质送至富氢气闪蒸罐中闪蒸出富氢气送至第二换热器、第一换热器复温后出冷箱，后将富氢气闪蒸罐底部的液体经过节流阀节流后送至汽提塔中脱除剩余氢气；塔顶气体送至第二换热器、第一换热器复温后出冷箱，塔底液体经过节流后送至含有循环介质作冷源的脱氮塔中脱除氮气；脱氮塔顶部的富氮气经过第二换热器、第一换热器复温后出冷箱、脱氮塔底部的工艺液体经过节流后直接送至含有循环介质的脱甲烷塔脱除甲烷；脱甲烷塔底部的富甲烷液体经过第二换热器、第一换热器换热器复温后出冷箱，脱甲烷塔顶部的一氧化碳产品气送至换热器复温后出冷箱。
一般的工艺流程在脱氮塔需要有工艺液体之外的循环介质作冷源，同时，脱甲烷塔底部的液体需要外部循环介质的汽化；
发明内容
本实用新型的目的是克服现有技术的不足，提供一种利用工艺液体本身作为冷源的HyCO深冷分离装置节能优化系统。
一种HyCO深冷分离装置节能优化系统，其特征在于包括CO压缩机、脱氮塔顶冷凝器、脱氮塔、脱氮塔底工艺液体节流阀、脱甲烷塔、第二换热器、循环CO节流阀、汽提塔底至脱氮塔节流阀、富氢气闪蒸罐、富氢气闪蒸罐至汽提塔工艺液体节流阀、汽提塔、第一换热器、洗涤液节流阀；
系统接受来自上游的净化气，净化气管路经过第一换热器、第二换热器后与富氢气闪蒸罐相连，富氢气闪蒸罐用于分离出富氢气；出富氢气闪蒸罐的净化气管路经富氢气闪蒸罐至汽提塔工艺液体节流阀后与汽提塔的进料口相连；汽提塔顶部出料口分离出闪蒸汽流股，底部出料口通过输送管路经汽提塔底至脱氮塔节流阀后连接至脱氮塔进料口；
脱氮塔顶部出料口产出富氮气流股，富氮气流股顺次经脱氮塔顶冷凝器、第二换热器和第一换热器换热后离开系统；脱氮塔底部出料口通过管路经脱氮塔底工艺液体节流阀、脱氮塔顶冷凝器后连接至脱甲烷塔进料口，其中，脱氮塔底部工艺流体作为脱氮塔顶冷凝器的冷源；
脱甲烷塔底部出料口产出富甲烷气，富甲烷气流股再通过第二换热器、第一换热器换热后离开系统；脱甲烷塔顶部出料口产出CO产品气，CO产品气流股进入循环管线，所述的循环管线依此经过第二换热器、第一换热器、CO压缩机、第一换热器、第二换热器、循环CO节流阀后并再次进入第二换热器构成循环；循环管线由CO压缩机处产出加压的CO产品气和循环CO介质；循环CO介质部分从循环管线导出并通过洗涤液节流阀管路进入脱甲烷塔。
所述的一种HyCO深冷分离装置节能优化工艺系统，其特征在于富氢气闪蒸罐分离出的富氢气流股经第二换热器、第一换热器后离开系统。
本实用新型弥补了普通一种HyCO深冷分离装置节能优化系统领域存在的不足。使用本实用新型，利用工艺液体自身作为脱氮塔冷凝器的冷源，对整个工艺流程的环保及能耗方面做出重大贡献，一方面减少了脱氮塔顶冷凝器对循环介质的需求，另一方面减小了脱甲烷塔底再沸器对循环介质的需求，从而优化了装置流程，降低了装置能耗，节约成本。这不仅对生产有利好，而且符合我国节能减排的要求。
附图说明
图1为本实用新型一种HyCO深冷分离装置节能优化系统；
图2为本实用新型一种HyCO深冷分离装置节能优化系统的脱氮塔冷凝流程；
图3为本实用新型一种HyCO深冷分离装置节能优化系统的脱甲烷塔流程；
图中，CO压缩机1、脱氮塔顶冷凝器2、脱氮塔3、脱氮塔底工艺液体节流阀4、脱甲烷塔5、第二换热器6、循环CO节流阀7、汽提塔底至脱氮塔节流阀8、富氢气闪蒸罐9、富氢气闪蒸罐至汽提塔工艺液体节流阀10、汽提塔11、第一换热器12、洗涤液节流阀13。
具体实施方式
如图1所示，一种HyCO深冷分离装置节能优化系统，包括CO压缩机1、脱氮塔顶冷凝器2、脱氮塔3、脱氮塔底工艺液体节流阀4、脱甲烷塔5、第二换热器6、循环CO节流阀7、汽提塔底至脱氮塔节流阀8、富氢气闪蒸罐9、富氢气闪蒸罐至汽提塔工艺液体节流阀10、汽提塔11、第一换热器12、洗涤液节流阀13；
根据本实用新型的一个具体实施例，系统接受来自上游的净化气，净化气管路经过第一换热器12、第二换热器6后与富氢气闪蒸罐9相连，富氢气闪蒸罐用于分离出富氢气；出富氢气闪蒸罐的净化气管路经富氢气闪蒸罐至汽提塔工艺液体节流阀10后与汽提塔11的进料口相连；汽提塔11顶部出料口分离出闪蒸汽流股，底部出料口通过输送管路经汽提塔底至脱氮塔节流阀8后连接至脱氮塔3进料口；
如图2、3所示，根据本实用新型的一个具体实施例，脱氮塔3顶部出料口产出富氮气流股，富氮气流股顺次经脱氮塔顶冷凝器2、第二换热器6和第一换热器12换热后离开系统；脱氮塔3底部出料口通过管路经脱氮塔底工艺液体节流阀4、脱氮塔顶冷凝器2后连接至脱甲烷塔5进料口，其中，脱氮塔3底部工艺流体作为脱氮塔顶冷凝器2的冷源；
脱甲烷塔5底部出料口产出富甲烷气，富甲烷气流股再通过第二换热器6、第一换热器12换热后离开系统；脱甲烷塔5顶部出料口产出CO产品气，CO产品气流股进入循环管线，所述的循环管线依此经过第二换热器6、第一换热器12、CO压缩机1、第一换热器12、第二换热器6、循环CO节流阀7后并再次进入第二换热器6；循环管线由CO压缩机1处产出加压的CO产品气和循环CO介质；循环CO介质通过洗涤液节流阀13管路进入脱甲烷塔5。
所述系统的HyCO深冷分离装置节能优化工艺，其特征在于包括以下步骤：
1)上游的净化气经过第一换热器12、第二换热器6降温后被送至富氢气闪蒸罐9，分离出富氢气；
2)出富氢气闪蒸罐9的净化气经过富氢气闪蒸罐至汽提塔工艺液体节流阀10被送至汽提塔11，分离出闪蒸汽，再通过第二换热器6、第一换热器12出冷箱；
3)出汽提塔11的净化气经过汽提塔底至脱氮塔节流阀8被送至脱氮塔3，分离出富氮气，再通过第二换热器6、第一换热器12出冷箱；脱氮塔3底部温度约为-163℃，顶部温度约为-164.5℃。由于出脱氮塔3底部的工艺液体压力约为1MPaG，HyCO深冷分离装置产品出冷箱的压力要求约0.7MPa，脱氮塔3底部工艺液体从1.0MPa节流至0.7MPa时温度由-163℃降至-166.5℃，可以满足脱氮塔3顶部冷源温度需求。所以，被送至脱氮塔3出脱氮塔底的工艺液体经脱氮塔底工艺液体节流阀4后被送至脱氮塔顶冷凝器2作冷源，气化后被送至脱甲烷塔5；
4)出脱氮塔顶冷凝器2的气体经脱甲烷塔5处理后，分离出富甲烷气，再通过第二换热器6、第一换热器12出冷箱；
5)从脱甲烷塔(5)顶部分离出的CO产品气进入循环管线，循环管线由CO压缩机(1)处产出加压的CO产品气和循环CO介质；
6)循环CO介质部分从循环管线导出并通过洗涤液节流阀(13)回到脱甲烷塔(5)。
本实施例利用工艺液体自身作为脱氮塔冷凝器的冷源，脱氮塔3底部工艺液体经节流后温度降低，满足脱氮塔3顶部冷源温度需求，本实用新型降低了整个工艺流程的能耗，即减少了脱氮塔顶冷凝器对循环介质的需求，又减小了脱甲烷塔底再沸器对循环介质的需求，从而优化了装置流程，降低了装置能耗，节约成本。

Claims (2)

1.一种HyCO深冷分离装置节能优化系统，其特征在于包括CO压缩机(1)、脱氮塔顶冷凝器(2)、脱氮塔(3)、脱氮塔底工艺液体节流阀(4)、脱甲烷塔(5)、第二换热器(6)、循环CO节流阀(7)、汽提塔底至脱氮塔节流阀(8)、富氢气闪蒸罐(9)、富氢气闪蒸罐至汽提塔工艺液体节流阀(10)、汽提塔(11)、第一换热器(12)、洗涤液节流阀(13)；
系统接受来自上游的净化气，净化气管路经过第一换热器(12)、第二换热器(6)后与富氢气闪蒸罐(9)相连，富氢气闪蒸罐用于分离出富氢气；出富氢气闪蒸罐的净化气管路经富氢气闪蒸罐至汽提塔工艺液体节流阀(10)后与汽提塔(11)的进料口相连；汽提塔(11)顶部出料口分离出闪蒸汽流股，底部出料口通过输送管路经汽提塔底至脱氮塔节流阀(8)后连接至脱氮塔(3)进料口；
脱氮塔(3)顶部出料口产出富氮气流股，富氮气流股顺次经脱氮塔顶冷凝器(2)、第二换热器(6)和第一换热器(12)换热后离开系统；脱氮塔(3)底部出料口通过管路经脱氮塔底工艺液体节流阀(4)、脱氮塔顶冷凝器(2)后连接至脱甲烷塔(5)进料口，其中，脱氮塔(3)底部工艺流体作为脱氮塔顶冷凝器(2)的冷源；
脱甲烷塔(5)底部出料口产出富甲烷气，富甲烷气流股再通过第二换热器(6)、第一换热器(12)换热后离开系统；脱甲烷塔(5)顶部出料口产出CO产品气，CO产品气流股进入循环管线，所述的循环管线依此经过第二换热器(6)、第一换热器(12)、CO压缩机(1)、第一换热器(12)、第二换热器(6)、循环CO节流阀(7)后并再次进入第二换热器(6)构成循环；循环管线由CO压缩机(1)处产出加压的CO产品气和循环CO介质；循环CO介质部分从循环管线导出并通过洗涤液节流阀(13)管路进入脱甲烷塔(5)。
2.根据权利要求1所述的一种HyCO深冷分离装置节能优化系统，其特征在于富氢气闪蒸罐分离出的富氢气流股经第二换热器(6)、第一换热器(12)后离开系统。
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CN110553463A (zh) * 2019-08-29 2019-12-10 杭州中泰深冷技术股份有限公司 一种HyCO深冷分离装置节能优化系统及其工艺

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110553463A (zh) * 2019-08-29 2019-12-10 杭州中泰深冷技术股份有限公司 一种HyCO深冷分离装置节能优化系统及其工艺

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