CN114593559B - 一种应用于flng的bog精馏脱氮装置 - Google Patents

一种应用于flng的bog精馏脱氮装置 Download PDF

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CN114593559B
CN114593559B CN202011411566.5A CN202011411566A CN114593559B CN 114593559 B CN114593559 B CN 114593559B CN 202011411566 A CN202011411566 A CN 202011411566A CN 114593559 B CN114593559 B CN 114593559B
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denitrification
bog
outlet
rectification
condenser
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CN114593559A (zh
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江浩
刘晓刚
林淑勤
吴本勇
邓林
赵卫军
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Wison Clean Energy Technology Group Co ltd
Shanghai Wison Offshore and Marine Co Ltd
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Abstract

本发明公开一种应用于FLNG的BOG精馏脱氮装置，包括冷箱、冷凝器、脱氮塔和再沸器，BOG进入冷箱冷却后进入脱氮塔精馏，脱氮塔顶部富氮气体经过冷凝器冷凝，抽出一股LNG产品，节流后进入脱氮塔顶冷凝器，作为冷凝器的冷源；冷凝后的富氮气体进入冷箱复热后直接排入大气；塔底气体物料经过再沸器处理后返回脱氮塔，脱氮塔底重沸器的热源为抽出的一股进料气，塔底气体为富甲烷气体，塔底富甲烷气体过冷后与LNG产品混合后送入LNG储罐。本发明采用精馏的方法脱除BOG气体中氮气，回收甲烷，从而制造出品质更高的LNG。本发明造价成本更低、能源消耗更少、更加有利于环保。

Description

一种应用于FLNG的BOG精馏脱氮装置
技术领域
本发明涉及化工技术领域，具体涉及一种应用于FLNG的BOG精馏脱氮装置。
背景技术
随着世界寻求更清洁的能源以减少污染和二氧化碳排放，液化天然气(LNG)需求未来几 十年将稳步增长，而FLNG装置的气源通常包含氮气，氮气含量随产地的不同而不同。该气 源液化后，BOG中会含有大量氮气，如果这部分氮气不从装置中脱除，将在系统中集聚而显 著降低FLNG装置的效率：1)由于其热值太低，不能作为FLNG装置燃机的燃料气去消耗掉进 气中的氮气；2)如果直接排放，将损失大量甲烷；3)如果FLNG中含有大量的液态氮气，将 增加FLNG运输的成本。
发明内容
本发明要解决的技术问题是提供一种应用于FLNG的BOG精馏脱氮装置，采用精馏的方 法脱除BOG气体中氮气，回收甲烷。
为解决上述技术问题，本发明采取如下技术方案：一种应用于FLNG的BOG精馏脱氮装 置，包括冷箱、冷凝器、脱氮塔和再沸器；所述的冷箱上设置有BOG入口、BOG出口、富氮气入口、富氮气出口、LNG出口、物料入口和富甲烷气体出口；BOG通过BOG入口进入冷箱；BOG出口通过管道与脱氮塔中部连接，BOG进入冷箱冷却到后进入脱氮塔中部进行精馏处理； 所述的脱氮塔顶部设置冷凝器；脱氮塔顶部的气体进入冷凝器；所述的冷凝器的气体排出口 通过管道与冷箱上的富氮气入口连接；进入冷箱的富氮气复热后从富氮气出口排出；所述的 LNG出口连接LNG储罐和冷凝器的冷源入口，冷凝器的冷源出口连接LNG储罐；所述脱氮塔 的下部设置有塔底流出物出口和返回物入口；所述的再沸器设置塔底流出物入口和返回物出 口；所述的塔底流出物出口通过管道与再沸器上的底流出物入口连接；所述的再沸器的返回 物出口通过管道与脱氮塔上的返回物入口连接；所述的脱氮塔的底部设置物料出口；所述的 物料出口通过管道与冷箱底部的物料入口连接；所述的富甲烷气体出口通过管道与LNG储罐 连接。
进一步地，所述的LNG出口连接出料管；出料管通过冷源管道与冷凝器的冷源入口连接， 出料管通过输送管道与LNG储罐连接；所述的冷源管道和所述的输送管道上均设置有节流阀； 所述的冷凝器的冷源出口通过管道与LNG储罐连接；所述的富甲烷气体出口通过管道与输送 管道连接。
进一步地，所述的再沸器的热源入口与BOG进料管道连接。
本发明还提供一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：具体为：BOG进 入冷箱冷却后进入脱氮塔精馏，脱氮塔顶部富氮气体经过冷凝器冷凝，抽出一股LNG产品， 节流后进入脱氮塔顶冷凝器，作为冷凝器的冷源；冷凝后的富氮气体进入冷箱复热后直接排 入大气；塔底气体物料经过再沸器处理后返回脱氮塔，脱氮塔底重沸器的热源为抽出的一股 进料气，塔底气体为富甲烷气体，塔底富甲烷气体过冷后与LNG产品混合后送入LNG储罐。
进一步地，BOG进入冷箱冷却到-150。
进一步地，脱氮塔精馏压力为2.2MPa。
进一步地，塔顶气体为富氮气体，冷凝至温度为-155℃，进入冷箱复热到30℃后直接 排入大气。
进一步地，塔底气体为富甲烷气体，温度为-106℃，进入冷箱过冷到-155℃与LNG产 品混合后送入LNG储罐。
本发明的有益效果为：本发明采用精馏的方法脱除BOG气体中氮气，回收甲烷，本发明 造价成本更低、能源消耗更少、更加有利于环保。
附图说明
下面结合附图和实施例对本发明作进一步说明。
图1是本发明的结构示意图。
具体实施方式
下面将通过具体实施方式对本发明的技术方案进行清楚、完整地描述。
参考图1为本发明的一种应用于FLNG的BOG精馏脱氮装置，包括冷箱1、冷凝器2、脱氮塔3和再沸器4；所述的冷箱1上设置有BOG入口11、BOG出口12、富氮气入口13、 富氮气出口14、LNG出口15、物料入口16和富甲烷气体出口17；BOG通过BOG入口11进 入冷箱1；BOG出口12通过管道与脱氮塔3中部连接，BOG进入冷箱冷却到后进入脱氮塔 中部进行精馏处理；所述的脱氮塔3顶部设置冷凝器2；脱氮塔3顶部的气体进入冷凝器 2；所述的冷凝器2的气体排出口通过管道与冷箱1上的富氮气入口13连接；进入冷箱 1的富氮气复热后从富氮气出口14排出；所述的LNG出口15连接LNG储罐5和冷凝器 2的冷源入口，冷凝器2的冷源出口连接LNG储罐5；所述脱氮塔3的下部设置有塔底流出 物出口31和返回物入口32；所述的再沸器4设置塔底流出物入口41和返回物出口42；所 述的塔底流出物出口31通过管道与再沸器上的底流出物入口41连接；所述的再沸器的返 回物出口42通过管道与脱氮塔上的返回物入口32连接；所述的脱氮塔3的底部设置物料 出口33；所述的物料出口33通过管道与冷箱底部的物料入口16连接；所述的富甲烷气体 出口17通过管道与LNG储罐5连接。
本发明的LNG出口15连接出料管6；出料管6通过冷源管道7与冷凝器2的冷源入口连接，出料管6通过输送管道8与LNG储罐5连接；所述的冷源管道7和所述的输送管道8 上均设置有节流阀9；所述的冷凝器2的冷源出口通过管道与LNG储罐5连接；所述的富甲 烷气体出口17通过管道与输送管道8连接。
本发明的再沸器4的热源入口与BOG进料管道连接。
本发明的冷箱1上还设置高压冷机入口18和低压冷剂出口19。
本发明还提供一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：具体为：BOG进 入冷箱冷却到-155℃后进入脱氮塔精馏，脱氮塔顶部富氮气体经过冷凝器冷凝，脱氮塔精馏 压力为2.2MPa。抽出一股LNG产品，节流后进入脱氮塔顶冷凝器，作为冷凝器的冷源。塔 顶气体为富氮气体，冷凝至温度为-155℃，进入冷箱复热到30℃后直接排入大气。塔底气 体物料经过再沸器处理后返回脱氮塔，脱氮塔底重沸器的热源为抽出的一股进料气，塔底气 体为富甲烷气体，温度为-106℃，进入冷箱过冷到-155℃与LNG产品混合后送入LNG储罐。
以上所述，仅是本发明的较佳实施例而已，不用于限制本发明，本领域技术人员可以在 本发明的实质和保护范围内，对本发明做出各种修改或等同替换，这种修改或等同替换也应 视为落在本发明技术方案的保护范围内。

Claims (8)

1.一种应用于FLNG的BOG精馏脱氮装置，其特征在于：包括冷箱(1)、冷凝器(2)、脱氮塔(3)和再沸器(4)；所述的冷箱(1)上设置有BOG入口(11)、BOG出口(12)、富氮气入口(13)、富氮气出口(14)、LNG出口(15)、物料入口(16)和富甲烷气体出口(17)；BOG通过BOG入口(11)进入冷箱(1)；BOG出口(12)通过管道与脱氮塔(3)中部连接，BOG进入冷箱冷却到特定温度后进入脱氮塔中部进行精馏处理；所述的脱氮塔(3)顶部设置冷凝器(2)；脱氮塔(3)顶部的气体进入冷凝器(2)；所述的冷凝器(2)的气体排出口通过管道与冷箱(1)上的富氮气入口(13)连接；进入冷箱(1)的富氮气复热进行冷能回收后从富氮气出口(14)排出；所述的LNG出口(15)连接LNG储罐(5)和冷凝器(2)的冷源入口，冷凝器(2)的冷源出口连接LNG储罐(5)；所述脱氮塔(3)的下部设置有塔底流出物出口(31)和返回物入口(32)；所述的再沸器(4)设置塔底流出物入口(41)和返回物出口(42)；所述的塔底流出物出口(31)通过管道与再沸器上的底流出物入口(41)连接；所述的再沸器的返回物出口(42)通过管道与脱氮塔上的返回物入口(32)连接；所述的脱氮塔(3)的底部设置物料出口(33)；所述的物料出口(33)通过管道与冷箱底部的物料入口(16)连接；所述的富甲烷气体出口(17)通过管道与LNG储罐(5)连接。
2.根据权利要求1所述的一种应用于FLNG的BOG精馏脱氮装置，其特征在于：所述的LNG出口(15)连接出料管(6)；出料管(6)通过冷源管道(7)与冷凝器(2)的冷源入口连接，出料管(6)通过输送管道(8)与LNG储罐(5)连接；所述的冷源管道(7)和所述的输送管道(8)上均设置有节流阀(9)；所述的冷凝器(2)的冷源出口通过管道与LNG储罐(5)连接；所述的富甲烷气体出口(17)通过管道与输送管道(8)连接。
3.根据权利要求1所述的一种应用于FLNG的BOG精馏脱氮装置，其特征在于：所述的再沸器(4)的热源入口与BOG进料管道连接。
4.采用权利要求1所述的一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：其特征在于：BOG进入冷箱冷却后进入脱氮塔精馏，脱氮塔顶部富氮气体经过冷凝器冷凝.抽出一股LNG产品，自管道7节流后进入脱氮塔顶冷凝器，作为冷凝器的冷源；冷凝后的富氮气体进入冷箱复热进行冷能回收后直接排入大气；塔底气体物料经过再沸器处理后返回脱氮塔，脱氮塔底重沸器的热源为抽出的一股进料气，塔底气体为富甲烷气体，塔底富甲烷气体过冷后与LNG产品混合后送入LNG储罐。
5.根据权利要求4所述的一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：其特征在于：BOG进入冷箱冷却到-150℃。
6.根据权利要求4所述的一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：其特征在于：脱氮塔精馏压力为2.2MPa。
7.根据权利要求4所述的一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：其特征在于：塔顶气体为富氮气体，冷凝至温度为-155℃，进入冷箱复热到30℃后直接排入大气。
8.根据权利要求4所述的一种应用于FLNG的BOG精馏脱氮装置的精馏脱氮方法：其特征在于：塔底气体为富甲烷气体，温度为-106℃，进入冷箱过冷到-155℃与LNG产品混合后送入LNG储罐。
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