CN108106325A - 适用于海上的天然气液化*** - Google Patents

适用于海上的天然气液化*** Download PDF

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CN108106325A
CN108106325A CN201810014919.4A CN201810014919A CN108106325A CN 108106325 A CN108106325 A CN 108106325A CN 201810014919 A CN201810014919 A CN 201810014919A CN 108106325 A CN108106325 A CN 108106325A
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heat exchanger
main
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CN108106325B (zh
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季鹏
郑雪枫
李婵
陈振中
潘红宇
赵甲递
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China Huanqiu Engineering Co Ltd
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Abstract

本发明提供一种适用于海上的天然气液化***，包括轻烃分离装置、混合制冷剂预冷循环、预冷主低温换热器、混合制冷剂深冷循环、一号深冷主低温换热器与二号深冷主低温换热器，所述轻烃分离装置包括脱甲烷塔，所述脱甲烷塔的塔顶气经脱甲烷塔冷箱、膨胀压缩机后依次与所述预冷主低温换热器、一号深冷主低温换热器以及二号深冷主低温换热器形成换热接触，再通过主节流阀之后进入LNG闪蒸罐，LNG闪蒸罐能够分离出的LNG与BOG；所述混合制冷剂预冷循环与所述预冷主低温换热器形成换热接触；所述混合制冷剂深冷循环与所述一号深冷主低温换热器以及二号深冷主低温换热器分别形成换热接触。本发明能够减少液化***的能量消耗，降低***压力，减少丙烷泄露风险。

Description

适用于海上的天然气液化***
技术领域
本发明涉及一种FLNG(Floating Liquefied Natural Gas又称为LNG-FPSO)***。
背景技术
天然气资源广泛分布在全球的陆地及海洋中，从陆地到海洋是世界油气勘探开发的必然趋势。FLNG(Floating Liquefied Natural Gas又称为LNG-FPSO)是近年来海洋工程界提出的，集液化天然气的生产、储存和装卸为一体的新型海上装置，对于海上气田的开采具有建造周期短、开发风险小，便于迁移和安全性高等特点。
海上作业需考虑台风、波浪、空间限制等不利因素，使得浮式天然气液化工艺的技术难度高于陆上。作为FLNG的核心技术，天然气液化工艺的合理性对工程项目的投资成本、运行费用、运营可靠性以及生产安全至关重要。针对海上工况的特殊性，由于级联式液化工艺所需设备数量较多，紧凑性不高，制冷剂的储存量较大，因此用于海上天然气液化有一定的困难。而混合制冷剂液化工艺和氮膨胀液化工艺海上适应性较好。
现有技术中丙烷预冷双氮膨胀天然气液化***大量使用丙烷作为制冷剂，丙烷具有沸点低、易汽化的特点，开停车操作时，设备和管线中存在大量丙烷会导致压力升高，增大丙烷泄放或泄漏的风险。一旦发生泄漏，由于丙烷的密度大于空气，会造成可燃气体的积聚，并且FLNG上部甲板空间有限、设备紧凑，扩散条件差，极易发生燃烧、***等事故。对于海上的天然气液化***，避免丙烷的使用能够提高安全性，减少安全设施的投资。
海上气田天然气的产量和组分不断改变，外部环境始终在变化，并且FLNG装置应具有可迁移性，这就要求天然气液化***具有灵活的可调节性，可以根据实际情况调节预冷段、深冷段负荷，减少冷热流体的换热温差，降低液化功耗。现有技术中双氮膨胀循环的压力均为8MPa，无法调节不同温区的换热温差，可调节性差，能耗高。
现有技术中经膨胀机增压机和压缩机增压后的氮气压力高达8MPa，设备和管线的压力等级高，工艺设备的重量增加，管架等支撑结构的载重增加，对船体结构的强度等提出更高要求，造成上部工艺模块和船体的造价大幅上升，降低了项目的经济性。
发明内容
为克服现有浮式天然气液化技术安全性低、可调节性差、能耗高、经济性差的缺点，本发明提出一种天然气液化***，能够实现不同海域、不同气质条件下稳定高效的轻烃分离和液化天然气生产。
为实现上述目的，本发明采用的技术方案是：
一种适用于海上的天然气液化***，其特征是包括轻烃分离装置、混合制冷剂预冷循环、预冷主低温换热器、混合制冷剂深冷循环、一号深冷主低温换热器与二号深冷主低温换热器，其中：
所述轻烃分离装置包括脱甲烷塔，所述脱甲烷塔的塔顶气依次与所述预冷主低温换热器、一号深冷主低温换热器以及二号深冷主低温换热器形成换热接触，再通过主节流阀之后进入LNG闪蒸罐，LNG闪蒸罐能够分离出的LNG与BOG；
所述混合制冷剂预冷循环与所述预冷主低温换热器形成换热接触；
所述混合制冷剂深冷循环与所述一号深冷主低温换热器以及二号深冷主低温换热器分别形成换热接触。
所述的适用于海上的天然气液化***，其中：所述混合制冷剂预冷循环包括依次循环连接的预冷缓冲罐、预冷压缩机、预冷水冷器以及预冷节流阀，所述预冷水冷器与所述预冷节流阀之间的管路与所述预冷主低温换热器形成换热接触，所述预冷节流阀与所述预冷缓冲罐之间的管路也与所述预冷主低温换热器形成换热接触。
所述的适用于海上的天然气液化***，其中：所述混合制冷剂深冷循环包括深冷缓冲罐、深冷压缩机、深冷水冷器、深冷分离罐、一号深冷节流阀与二号深冷节流阀，所述深冷缓冲罐、深冷压缩机、深冷水冷器、深冷分离罐依次连接，而且所述深冷水冷器与所述深冷分离罐之间的管路与所述预冷主低温换热器形成换热接触，所述深冷分离罐的液相管路与所述一号深冷主低温换热器形成换热接触，再与所述一号深冷节流阀相连通，所述深冷分离罐的气相管路依次与所述一号深冷主低温换热器以及所述二号深冷主低温换热器形成换热接触，再与所述二号深冷节流阀相连通，二号深冷节流阀的下游管路与所述二号深冷主低温换热器形成换热接触之后，再与所述一号深冷节流阀的下游管路合并，合并后的回流管路与所述一号深冷主低温换热器形成换热接触之后，回流到所述深冷缓冲罐。
所述的适用于海上的天然气液化***，其中：所述混合制冷剂预冷循环使用的预冷混合制冷剂含有乙烷至戊烷的轻烃，不含有丙烷以及碳六以上的组份；所述混合制冷剂深冷循环使用的深冷混合制冷剂中含有氮气、甲烷至戊烷的轻烃，不含有丙烷以及碳六以上的组分。
所述的适用于海上的天然气液化***，其中：所述轻烃分离装置包括一段冷箱、二段冷箱、低温分离罐以及膨胀压缩机，所述一段冷箱的一路进气口可供原料气进入，一段冷箱的一路出气口与所述低温分离罐相接，所述低温分离罐的气相出口与所述膨胀压缩机的膨胀端相连，再与所述低温分离罐的液相出口汇合后与所述脱甲烷塔的入口相连；所述低温分离罐的气相出口还与所述二段冷箱的一路进气口相接，所述二段冷箱的一路出气口也连通至所述脱甲烷塔；所述脱甲烷塔的塔顶连通至所述二段冷箱的另一路进气口，所述二段冷箱的另一路出气口则与所述一段冷箱的另一路进气口相连通，所述一段冷箱的另一路出气口连通至所述膨胀压缩机的压缩端，再依次与所述预冷主低温换热器、一号深冷主低温换热器以及二号深冷主低温换热器形成换热接触。
所述的适用于海上的天然气液化***，其中：所述轻烃分离装置还包括依次连接的脱乙烷塔、脱丙烷塔和脱丁烷塔，所述脱甲烷塔的塔底气依次与所述脱乙烷塔、脱丙烷塔和脱丁烷塔相接，所述脱丙烷塔的塔顶产品回注进入原料气。
本发明基于海上作用的特殊性，提出了一种适用于海上的天然气液化***，优化了混合制冷剂预冷循环、混合制冷剂深冷循环、轻烃分离塔的工艺参数；预冷混合制冷剂和深冷混合制冷剂均不包含丙烷，提高了安全性；减少了液化***的能量消耗，针对不同的气质条件和海洋环境，液化率达到96％，相比于现有技术丙烷预冷双氮膨胀天然气液化***，比功耗降低约10％。
附图说明
图1是本发明提供的适用于海上的天然气液化***的结构原理图。
附图标记说明：1轻烃分离装置，11脱甲烷塔，12脱乙烷塔，13脱丙烷塔，14脱丁烷塔，15脱甲烷塔一段冷箱，16脱甲烷塔二段冷箱，17低温分离罐，18膨胀压缩机，2混合制冷剂预冷循环，21预冷缓冲罐，22预冷压缩机，23预冷水冷器，3混合制冷剂深冷循环，31深冷缓冲罐，32深冷压缩机，33深冷水冷器，34深冷分离罐，4主节流阀，5预冷节流阀，6一号深冷节流阀，7二号深冷节流阀，8-LNG闪蒸罐，91预冷主低温换热器，92一号深冷主低温换热器，93二号深冷主低温换热器。
具体实施方式
如图1所示，本发明提供一种适用于海上的天然气液化***，其包括轻烃分离装置1、混合制冷剂预冷循环2、预冷主低温换热器91、混合制冷剂深冷循环3、一号深冷主低温换热器92与二号深冷主低温换热器93，其中：
所述轻烃分离装置1主要包括依次连接的脱甲烷塔11、脱乙烷塔12、脱丙烷塔13和脱丁烷塔14，能够顺序脱除天然气中的甲烷、乙烷、丙烷和丁烷，所述脱乙烷塔12的塔顶连接乙烷储罐，所述脱丁烷塔14的塔顶和塔底分别连接丁烷储罐和凝析油储罐，本发明不设置丙烷存储，脱丙烷塔13的塔顶产品的丙烷摩尔分数约96％，塔顶产品回注进入原料气。脱甲烷塔11所需要的冷量来自于脱甲烷塔一段冷箱15、脱甲烷塔二段冷箱16、低温分离罐17和膨胀压缩机18，并不涉及天然气液化***，因此该发明的工艺技术流程简单，设备布置紧凑，便于成撬，并且对原料气组成的变化适应性大。
其中，所述轻烃分离装置1还包括一段冷箱15、二段冷箱16、低温分离罐17以及膨胀压缩机18，所述一段冷箱15的一路进气口可供原料气进入，一段冷箱16的一路出气口与所述低温分离罐17相接，所述低温分离罐17的气相出口与所述膨胀压缩机18的膨胀端相连，通过膨胀降温后与所述低温分离罐17的液相出口汇合然后进入所述脱甲烷塔11；所述低温分离罐17的气相出口还与所述二段冷箱16的一路进气口相接，所述二段冷箱16的一路出气口也连通至所述脱甲烷塔11；所述脱甲烷塔11的塔顶连通至所述二段冷箱16的另一路进气口，所述二段冷箱16的另一路出气口则与所述一段冷箱15的另一路进气口相连通，所述一段冷箱15的另一路出气口连通至所述膨胀压缩机18的压缩端进行增压，增压后依次与所述预冷主低温换热器91、一号深冷主低温换热器92以及二号深冷主低温换热器93形成换热接触之后，通过主节流阀4之后进入LNG闪蒸罐8，LNG闪蒸罐8分离出的LNG储存以等待外运，分离出的BOG进入燃料气***；所述脱甲烷塔11的塔底产品依次进入脱丙烷塔13脱乙烷塔12、脱丙烷塔13和脱丁烷塔14，就不再赘述了。如此设置，可使脱甲烷塔11所需要的冷量来自于轻烃分离装置1自身。
所述混合制冷剂预冷循环2包括依次循环连接的预冷缓冲罐21、预冷压缩机22、预冷水冷器23以及预冷节流阀5，所述预冷水冷器23与所述预冷节流阀5之间的管路与所述预冷主低温换热器91形成换热接触，所述预冷节流阀5与所述预冷缓冲罐21之间的管路也与所述预冷主低温换热器91形成换热接触。
所述混合制冷剂深冷循环3包括深冷缓冲罐31、深冷压缩机32、深冷水冷器33、深冷分离罐34、一号深冷节流阀6与二号深冷节流阀7，所述深冷缓冲罐31、深冷压缩机32、深冷水冷器33、深冷分离罐34依次连接，而且所述深冷水冷器33与所述深冷分离罐34之间的管路与所述预冷主低温换热器91形成换热接触，所述深冷分离罐34的液相管路与所述一号深冷主低温换热器92形成换热接触，再与所述一号深冷节流阀6相连通，所述深冷分离罐34的气相管路依次与所述一号深冷主低温换热器92以及所述二号深冷主低温换热器93形成换热接触，再与所述二号深冷节流阀7相连通，二号深冷节流阀7的下游管路与所述二号深冷主低温换热器93形成换热接触之后，再与所述一号深冷节流阀6的下游管路合并，合并后的回流管路与所述一号深冷主低温换热器92形成换热接触之后，回流到所述深冷缓冲罐31。
混合制冷剂预冷循环2与混合制冷剂深冷循环3中所用的制冷剂组分不同，预冷混合制冷剂含有乙烷至戊烷的轻烃组成，不含有丙烷以及碳六以上的组份；深冷混合制冷剂中含有氮气、甲烷至戊烷的轻烃组成，不含有丙烷以及碳六以上的组分。
下面以一个较佳实施例，详细介绍本发明的工作过程如下：
脱除固体颗粒、水、酸性气体、汞、苯等杂质后，原料气进入一段冷箱15，冷却后进入低温分离罐17，分离后的部分气相原料气经膨胀压缩机18的膨胀端的膨胀降温，与液相原料气汇合后进入脱甲烷塔11，另一部分气相原料气经脱甲烷塔二段冷箱16冷却后进入脱甲烷塔11，脱甲烷塔11的塔顶产品甲烷摩尔分数约96％，塔顶产品经脱甲烷塔一段冷箱15、脱甲烷塔二段冷箱16升温，然后进入膨胀压缩机18的压缩端进行增压，增压后流入预冷主低温换热器91，脱甲烷塔11的塔底产品进入脱乙烷塔12；脱乙烷塔12的塔顶产品的乙烷摩尔分数约96％，塔底产品进入脱丙烷塔13；脱丙烷塔13的塔顶产品的丙烷摩尔分数约96％，塔顶产品回注进入原料气，塔底产品进入脱丁烷塔14；脱丁烷塔14塔顶产品的丁烷摩尔分数约92％，塔底产品凝析油作为副产品储存外运。
原料气经脱甲烷塔11后进入预冷主低温换热器91，经预冷混合制冷剂冷却至约-45℃～-52℃，然后依次流入一号深冷主低温换热器92和二号深冷主低温换热器93，经深冷混合制冷剂冷却至约-148℃～-156℃，通过主节流阀4节流降温至-160℃后流入LNG闪蒸罐8，分离出的LNG储存等待外运，BOG进入燃料气***。
预冷混合制冷剂经预冷压缩机22压缩至约3.8MPa～4.3MPa，压缩后经预冷水冷器23冷却，预冷水冷器23的冷源采用海水；预冷混合制冷剂压缩水冷后进入预冷主低温换热器91，经预冷节流阀5节流降温，然后返回预冷主低温换热器91，用以冷却原料气、深冷混合制冷剂和高温的预冷混合制冷剂；充分换热后，预冷混合制冷剂进入预冷缓冲罐21，形成混合制冷剂预冷循环。
深冷混合制冷剂经深冷压缩机32压缩至约3.9MPa～4.4MPa，压缩后经深冷水冷器33冷却，深冷水冷器33的冷源采用海水；深冷混合制冷剂压缩水冷后进入一号预冷主低温换热器91，预冷后进入深冷分离罐34；气液分离后的液相深冷混合制冷剂进入二号深冷主低温换热器，经一号深冷节流阀6节流降温；气液分离后的气相深冷混合制冷剂依次进入一号深冷主低温换热器92、二号深冷主低温换热器93，经二号深冷节流阀7节流降温，然后返回冷却原料气和气相深冷混合制冷剂，流出深冷主低温换热器93后与节流后的液相深冷混合制冷剂一起返回深冷主低温换热器92，用以冷却原料气和深冷混合制冷剂；充分换热后，深冷混合制冷剂进入深冷缓冲罐31，形成混合制冷剂深冷循环。
为保证液化***在海上晃荡条件下的稳定运行，对关键设备、工艺模块要求如下：预冷主低温换热器与深冷主低温换热器采用流体均布构件，优化内部换热结构，保证换热过程的稳定高效；气液分离器通过内部构件的设置，保证分离效果；根据工艺流程、关键设备型号尺寸、甲板空间等因素合理进行模块化划分，缩短建造周期。
以上说明对本发明而言只是说明性的，而非限制性的，本领域普通技术人员理解，在不脱离权利要求所限定的精神和范围的情况下，可作出许多修改、变化或等效，但都将落入本发明的保护范围之内。

Claims (6)

1.一种适用于海上的天然气液化***，其特征是包括轻烃分离装置、混合制冷剂预冷循环、预冷主低温换热器、混合制冷剂深冷循环、一号深冷主低温换热器与二号深冷主低温换热器，其中：
所述轻烃分离装置包括脱甲烷塔，所述脱甲烷塔的塔顶气依次与所述预冷主低温换热器、一号深冷主低温换热器以及二号深冷主低温换热器形成换热接触，再通过主节流阀之后进入LNG闪蒸罐，LNG闪蒸罐能够分离出的LNG与BOG；
所述混合制冷剂预冷循环与所述预冷主低温换热器形成换热接触；
所述混合制冷剂深冷循环与所述一号深冷主低温换热器以及二号深冷主低温换热器分别形成换热接触。
2.根据权利要求1所述的适用于海上的天然气液化***，其特征在于：所述混合制冷剂预冷循环包括依次循环连接的预冷缓冲罐、预冷压缩机、预冷水冷器以及预冷节流阀，所述预冷水冷器与所述预冷节流阀之间的管路与所述预冷主低温换热器形成换热接触，所述预冷节流阀与所述预冷缓冲罐之间的管路也与所述预冷主低温换热器形成换热接触。
3.根据权利要求1或2所述的适用于海上的天然气液化***，其特征在于：所述混合制冷剂深冷循环包括深冷缓冲罐、深冷压缩机、深冷水冷器、深冷分离罐、一号深冷节流阀与二号深冷节流阀，所述深冷缓冲罐、深冷压缩机、深冷水冷器、深冷分离罐依次连接，而且所述深冷水冷器与所述深冷分离罐之间的管路与所述预冷主低温换热器形成换热接触，所述深冷分离罐的液相管路与所述一号深冷主低温换热器形成换热接触，再与所述一号深冷节流阀相连通，所述深冷分离罐的气相管路依次与所述一号深冷主低温换热器以及所述二号深冷主低温换热器形成换热接触，再与所述二号深冷节流阀相连通，二号深冷节流阀的下游管路与所述二号深冷主低温换热器形成换热接触之后，再与所述一号深冷节流阀的下游管路合并，合并后的回流管路与所述一号深冷主低温换热器形成换热接触之后，回流到所述深冷缓冲罐。
4.根据权利要求1所述的适用于海上的天然气液化***，其特征在于：所述混合制冷剂预冷循环使用的预冷混合制冷剂含有乙烷至戊烷的轻烃，不含有丙烷以及碳六以上的组份；所述混合制冷剂深冷循环使用的深冷混合制冷剂中含有氮气、甲烷至戊烷的轻烃，不含有丙烷以及碳六以上的组分。
5.根据权利要求1所述的适用于海上的天然气液化***，其特征在于：所述轻烃分离装置包括一段冷箱、二段冷箱、低温分离罐以及膨胀压缩机，所述一段冷箱的一路进气口可供原料气进入，一段冷箱的一路出气口与所述低温分离罐相接，所述低温分离罐的气相出口与所述膨胀压缩机的膨胀端相连，再与所述低温分离罐的液相出口汇合后与所述脱甲烷塔的入口相连；所述低温分离罐的气相出口还与所述二段冷箱的一路进气口相接，所述二段冷箱的一路出气口也连通至所述脱甲烷塔；所述脱甲烷塔的塔顶连通至所述二段冷箱的另一路进气口，所述二段冷箱的另一路出气口则与所述一段冷箱的另一路进气口相连通，所述一段冷箱的另一路出气口连通至所述膨胀压缩机的压缩端，再依次与所述预冷主低温换热器、一号深冷主低温换热器以及二号深冷主低温换热器形成换热接触。
6.根据权利要求1或5所述的适用于海上的天然气液化***，其特征在于：所述轻烃分离装置还包括依次连接的脱乙烷塔、脱丙烷塔和脱丁烷塔，所述脱甲烷塔的塔底气依次与所述脱乙烷塔、脱丙烷塔和脱丁烷塔相接，所述脱丙烷塔的塔顶产品回注进入原料气。
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