CN104061755B - 一种用于天然气的脱氮装置及其脱氮工艺 - Google Patents

一种用于天然气的脱氮装置及其脱氮工艺 Download PDF

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CN104061755B
CN104061755B CN201410311707.4A CN201410311707A CN104061755B CN 104061755 B CN104061755 B CN 104061755B CN 201410311707 A CN201410311707 A CN 201410311707A CN 104061755 B CN104061755 B CN 104061755B
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heat exchanger
nitrogen
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compressor
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李贺松
董宪莹
王月娥
宋美萱
胡家乐
孔玉倩
高杨
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Tianjin Zenith Oil&gas Engineering Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/00—Processes or apparatus using separation by rectification
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Abstract

本发明公开了一种天然气中氮气的脱除工艺，包括以下步骤：LNG储罐中的BOG气体经过BOG冷箱复热后进入BOG增压***，增压至0.6～1.5Mpa；而后，BOG依次通过BOG冷箱和液化冷箱后将BOG冷却至-154℃～-165℃的液态，然后进入脱氮换热器进一步被冷却至-168～-176℃，再经过节流膨胀后温度降至-178～-185℃，进入氮气脱除设备分离出的氮气高点放空，净化后的天然气回收至LNG储罐。本发明通过对LNG储罐中的BOG深度冷却后脱除氮气，工艺成熟，适应性强，特别适合原料气中氮气含量较高且波动范围比较大的工况，能够部分回收LNG储罐放空的天然气，同时提高储罐储存的安全性。

Description

一种用于天然气的脱氮装置及其脱氮工艺
技术领域
本发明涉及一种天然气脱氮工艺及装置。
背景技术
随着清洁能源的应用意识逐渐增强，天然气的开发和应用越来越普遍。由于液化天然气(LNG)便于储存和运输，广泛应用于调峰站、公交车、重卡及船舶等。然而在天然气液化工厂中，有些气源的氮含量较高，使天然气液化困难，增大了液化过程的动力消耗；而且液化天然气产品中氮气含量高，对液化天然气的储存带来安全隐患。因此，脱除天然气中的氮气，保证进入LNG储罐中的天然气含氮量满足要求具有重要的实践意义。
发明内容
本发明的目的是提供一种天然气的脱氮工艺，通过设置BOG增压***、深冷***和氮气分离***，能够部分回收LNG储罐放空的天然气，同时提高储罐储存的安全性。本发明脱氮工艺是改造和优化天然气液化工艺的有效方法。
本发明一种用于天然气的脱氮装置，包括液态天然气储罐、BOG增压***、深冷***和氮气分离***；所述BOG增压***用于将BOG增压至0.6～1.5Mpa后冷却至35～55℃；所述BOG增压***包括依次相连的第一BOG压缩机、第一BOG换热器、第二BOG压缩机和第二BOG换热器；所述深冷***用于将BOG进一步冷却至-154℃～-165℃；所述深冷***包括BOG冷箱和液化冷箱，所述液态天然气储罐的闪蒸气出口通过所述BOG冷箱的冷流股通道连接至所述第一BOG压缩机的进口；所述第二BOG换热器的出口通过所述BOG冷箱的热流股通道后连接至所述液化冷箱的深冷通道；所述氮气分离***包括氮气脱除设备和脱氮换热器，所述液化冷箱的出口连接至所述脱氮换热器的热流股通道，位于所述氮气脱除设备底部的冷流股连接至所述脱氮换热器的冷流股通道，位于所述氮气脱除设备底部的冷流股出口连接至所述液态天然气储罐。
进一步讲，本发明用于天然气的脱氮装置，其中，所述第一BOG压缩机和第二BOG压缩机选用离心式压缩机、往复式压缩机和螺杆式压缩机中的一种；所述第一BOG换热器和所述第二BOG换热器选用翅片式换热器或管壳式换热器；所述BOG冷箱选用翅片式换热器或管壳式换热器；所述液化冷箱选用多流道板翅式冷箱或绕管式换热器；所述氮气脱除设备选用氮气分离器、氮气提馏塔和氮气闪蒸塔中的一种；所述脱氮换热器选用翅片式换热器、管壳式换热器或釜式再沸器。
本发明一种天然气中氮气的脱除工艺，包括以下步骤：
步骤一、液态天然气储罐中的BOG气体经过BOG冷箱复热后进入BOG增压***，通过第一BOG压缩机、第一BOG换热器、第二BOG压缩机和第二BOG换热器后将BOG气体增压至0.6～1.5Mpa，并冷却至35～55℃；
步骤二、经过BOG增压***处理后的BOG气体进入深冷***，依次通过BOG冷箱和液化冷箱后将BOG气体冷却至-154℃～-165℃的液态；
步骤三、经过深冷***处理后的液态BOG进入氮气分离***中的脱氮换热器，与氮气脱除设备底部流股进行换热，将液态BOG进一步冷却至-168～-176℃；
步骤四、经过脱氮换热器换热后的液态BOG经过一节流阀的节流膨胀后，液态BOG的温度降至-178～-185℃，液态BOG进入氮气脱除设备，氮气由氮气脱除设备分离后从顶部放空口排出；净化后的天然气由氮气脱除设备底部流出进入脱氮换热器作为冷源，与步骤三中深冷后的液态BOG进行换热，回收利用部分冷量后返回至液态天然气储罐。
与现有技术相比，本发明用于天然气的脱氮装置及其脱氮工艺的优点是：(1)原料气组分含氮量较高时，通过降低BOG中的氮气含量，可以有效降低LNG中含氮量，且能耗较低；(2)放空气中夹带的甲烷含量较低，减少资源的浪费。
附图说明
附图是本发明天然气中氮气的脱除工艺路线图。
具体实施方式
下面结合附图和具体实施例对本发明技术方案作进一步详细描述。
如附图所示，本发明一种用于天然气的脱氮装置，包括液态天然气储罐、BOG增压***、深冷***和氮气分离***。
所述BOG增压***用于将BOG增压至0.6～1.5Mpa后冷却至35～55℃；所述BOG增压***包括依次相连的第一BOG压缩机、第一BOG换热器、第二BOG压缩机和第二BOG换热器；所述第一BOG压缩机和第二BOG压缩机可以选用离心式压缩机、往复式压缩机和螺杆式压缩机中的一种，本实施例中选用的是螺杆式压缩机；所述第一BOG换热器和所述第二BOG换热器可以选用翅片式换热器或管壳式换热器，本实施例中选用的是管壳式换热器。
所述深冷***用于将BOG进一步冷却至-154℃～-165℃；所述深冷***包括BOG冷箱和液化冷箱，所述BOG冷箱选用翅片式换热器或管壳式换热器，本实施例中选用的是翅片式换热器；所述液化冷箱选用多流道板翅式冷箱或绕管式换热器，本实施例中选用的是多流道板翅式冷箱。
所述液态天然气储罐的闪蒸气出口通过所述BOG冷箱的冷流股通道连接至所述第一BOG压缩机的进口；所述第二BOG换热器的出口通过所述BOG冷箱的热流股通道后连接至所述液化冷箱的深冷通道。
所述氮气分离***包括氮气脱除设备和脱氮换热器，所述氮气脱除设备可以选用氮气分离器、氮气提馏塔和氮气闪蒸塔中的一种，本实施例中选用的是氮气提馏塔；所述脱氮换热器选用翅片式换热器、管壳式换热器或釜式再沸器，本实施例中选用的是釜式再沸器。
所述液化冷箱的出口连接至所述脱氮换热器的热流股通道，位于所述氮气脱除设备底部的冷流股连接至所述脱氮换热器的冷流股通道，位于所述氮气脱除设备底部的冷流股出口连接至所述液态天然气储罐。
利用本实施例的用于天然气的脱氮装置，实现天然气中氮气的脱除工艺过程如下：
液化天然气101进入液态天然气储罐V101中储存，储罐中产生的BOG气体102经过BOG冷箱E101复热至20℃左右后103进入第一BOG压缩机K1011一级增压至0.4Mpa104、经过第一BOG换热器E102冷却至40℃105，然后进入第二BOG压缩机K1012二级增压至0.97Mpa106，经过第二BOG换热器E103冷却至45℃107，进入BOG冷箱E101换热至-130℃108后再进入液化冷箱E104进一步冷却至-155℃左右109，继续进入氮气提馏塔T101塔底的釜式再沸器E105，进一步被冷却至-176℃110，经过节流阀VLV101节流膨胀，温度降至约-179℃111，进入氮气提馏塔T101脱除氮气，氮气由塔顶被分离出来复热后放空112，氮气提馏塔塔底流股进入釜式再沸器E105与流股109进行换热，塔底流股被复热，复热后气化部分返回至氮气提馏塔内，净化后的天然气由塔底流出113重新进入液态天然气储罐V101。
本实施例中各流股(附图中的附图标记为101、102、103、104、105、106、107、108、109、110、111、112、113)的具体参数见表1，表1中记载了各流股的温度、压力、流量及各组分的摩尔含量。
尽管上面结合附图对本发明进行了描述，但是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，而不是限制性的，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的情况下，还可以做出很多变形，这些均属于本发明的保护之内。

Claims (4)

1.一种用于天然气的脱氮装置，包括液态天然气储罐、BOG增压***、深冷***和氮气分离***；其特征在于：
所述BOG增压***用于将BOG增压至0.6～1.5Mpa后冷却至35～55℃；所述BOG增压***包括依次相连的第一BOG压缩机、第一BOG换热器、第二BOG压缩机和第二BOG换热器；
所述深冷***用于将BOG进一步冷却至-154℃～-165℃；所述深冷***包括BOG冷箱和液化冷箱，所述液态天然气储罐的闪蒸气出口通过所述BOG冷箱的冷流股通道连接至所述第一BOG压缩机的进口；所述第二BOG换热器的出口通过所述BOG冷箱的热流股通道后连接至所述液化冷箱的深冷通道；
所述氮气分离***包括氮气脱除设备和脱氮换热器，所述液化冷箱的出口连接至所述脱氮换热器的热流股通道，所述氮气脱除设备底部的冷流股通过所述脱氮换热器的冷流股通道，位于所述氮气脱除设备底部的冷流股出口连接至所述液态天然气储罐。
2.根据权利要求1所述用于天然气的脱氮装置，其中，
所述第一BOG压缩机和第二BOG压缩机选用离心式压缩机、往复式压缩机和螺杆式压缩机中的一种；
所述第一BOG换热器和所述第二BOG换热器选用翅片式换热器或管壳式换热器；
所述BOG冷箱选用翅片式换热器或管壳式换热器；
所述液化冷箱选用多流道板翅式冷箱；
所述氮气脱除设备选用氮气分离器、氮气提馏塔和氮气闪蒸塔中的一种；
所述脱氮换热器选用翅片式换热器、管壳式换热器和釜式再沸器中的一种。
3.根据权利要求1所述用于天然气的脱氮装置，其中，
所述第一BOG压缩机和第二BOG压缩机选用离心式压缩机、往复式压缩机和螺杆式压缩机中的一种；
所述第一BOG换热器和所述第二BOG换热器选用翅片式换热器或管壳式换热器；
所述BOG冷箱选用翅片式换热器或管壳式换热器；
所述液化冷箱选用绕管式换热器；
所述氮气脱除设备选用氮气分离器、氮气提馏塔和氮气闪蒸塔中的一种；
所述脱氮换热器选用翅片式换热器、管壳式换热器和釜式再沸器中的一种。
4.一种天然气中氮气的脱除工艺，其特征在于，采用如权利要求1所述用于天然气的脱氮装置，并包括以下步骤：
步骤一、液态天然气储罐中的BOG气体经过BOG冷箱复热后进入BOG增压***，通过第一BOG压缩机、第一BOG换热器、第二BOG压缩机和第二BOG换热器后将BOG气体增压至0.6～1.5Mpa，并冷却至35～55℃；
步骤二、经过BOG增压***处理后的BOG气体进入深冷***，依次通过BOG冷箱和液化冷箱后将BOG气体冷却至-154℃～-165℃的液态；
步骤三、经过深冷***处理后的液态BOG进入氮气分离***中的脱氮换热器，与氮气脱除设备底部流股进行换热，将液态BOG进一步冷却至-168～-176℃；
步骤四、经过脱氮换热器换热后的液态BOG经过一节流阀的节流膨胀后，液态BOG的温度降至-178～-185℃，液态BOG进入氮气脱除设备，氮气由氮气脱除设备分离后从顶部放空口排出；净化后的天然气由氮气脱除设备底部流出进入脱氮换热器作为冷源，与步骤三中深冷后的液态BOG进行换热，回收利用部分冷量后返回至液态天然气储罐。
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