CN110044131B - 一种多级压缩丙烷预冷天然气液化***及其液化方法 - Google Patents

一种多级压缩丙烷预冷天然气液化***及其液化方法 Download PDF

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CN110044131B
CN110044131B CN201910371416.7A CN201910371416A CN110044131B CN 110044131 B CN110044131 B CN 110044131B CN 201910371416 A CN201910371416 A CN 201910371416A CN 110044131 B CN110044131 B CN 110044131B
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heat exchanger
compressor
communicated
natural gas
propane
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CN110044131A (zh
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丁昌
吕林鹏
黄宇巍
顾华
李军旗
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Zhengzhou University of Light Industry
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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Abstract

本发明提出一种多级压缩丙烷预冷天然气液化***及其液化方法，包括丙烷预冷循环模块、混合制冷剂循环模块以及天然气液化模块；丙烷预冷循环模块即制冷剂丙烷经压缩、冷凝、节流后产生气液分离，液态冷剂节流降压进入预冷换热器提供冷量，再经压缩机增压至产生气液分离时的压力，与气液分离时的气态冷剂混合后进入压缩机；混合制冷剂循环模块即多组分混合制冷剂经逐级蒸发、冷凝、节流，使不同组分的冷剂在不同温区蒸发吸热，为天然气降温提供冷量；天然气液化模块即天然气经多级换热器降温至‑162℃成为液态。本发明采用多级压缩来改进丙烷预冷循环，降低了设备的运行功耗，结构简单、流程紧凑，对天然气液化过程的节能有重要意义。

Description

一种多级压缩丙烷预冷天然气液化***及其液化方法
技术领域
本发明涉及天然气液化，特别是指一种多级压缩丙烷预冷天然气液化***及其液化方法。
背景技术
天然气液化工艺发展到今天，种类已增加至数十种，但应用最为广泛的当属丙烷预冷混合制冷剂流程。天然气液化工艺是一种能量高度密集、成本高度密集的生产活动，其能耗占天然气开采、净化、液化、运输产业链总能耗的40%左右，对其进行***能耗的优化，对节能减排、减轻设备运负荷等方面大有裨益。现有制冷流程中，节流后的丙烷制冷剂产生气液分离，而气态丙烷制冷剂在换热器中无相变，因此换热效果较差。
发明内容
本发明提出一种多级压缩丙烷预冷天然气液化***及其液化方法，解决了现有丙烷预冷混合制冷剂流程换热效果差的问题。本发明主要针对预冷流程进行设，在预冷循环节流阀之后加上气液分离器，节流后的丙烷制冷剂产生气液分离，考虑到气态丙烷制冷剂在换热器中无相变因此换热效果略差，于是将这部分气态冷剂直接通入压缩机，以降低压缩机的吸气温度，液态丙烷制冷剂经节流降温后与混合冷剂、天然气换热后返回压缩机。本发明对传统的C3MR天然气液化流程进行分析，对***中㶲损较大的丙烷预冷循环进行优化设计，降低压缩机排气温度。设计的新流程***功耗小，改动成本低，经济可行性分析合理，具有较强的应用价值。
本发明的技术方案是这样实现的：一种多级压缩丙烷预冷天然气液化***，包括丙烷预冷循环模块和天然气液化模块，所述的丙烷预冷循环模块包括压缩机II，压缩机II出口与冷却器II连通，冷却器II与节流阀IV连通，节流阀IV与分离罐IV连通，分离罐IV一出口与节流阀V连通，节流阀V经过预冷换热器后与压缩机III连通，压缩机III与缓冲罐连通，分离罐IV另一出口与缓冲罐连通，缓冲罐与压缩机II进口连通。
所述的压缩机III与止回阀连通，止回阀与缓冲罐连通。
所述的分离罐IV另一出口与温度控制阀连通，温度控制阀感应压缩机II出口温度，温度控制阀与缓冲罐连通。
还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I，压缩机I与冷却器I连通，冷却器I经过预冷换热器后与分离罐I连通，分离罐I一出口经过中冷换热器后与节流阀II连通，节流阀II与分离罐II连通，分离罐I另一出口经过中冷换热器、深冷换热器后与节流阀III连通，节流阀III经过深冷换热器后与分离罐III连通，分离罐II的一出口与分离罐III的一出口合并，再与分离罐II的另一出口与分离罐III的另一出口合并后经过中冷换热器、预冷换热器的部分合并，然后与压缩机I连通。
所述的天然气液化模块包括液化管，液化管经过预冷换热器、中冷换热器和深冷换热器后与节流阀I连通。
一种多级压缩丙烷预冷天然气液化***的液化方法，包括丙烷预冷循环模块和天然气液化模块，所述的丙烷预冷循环模块包括压缩机II，丙烷制冷剂经过压缩机II压缩后，经冷却器II冷却至全液态，经节流阀IV节流降压降温后变为气液两相，在分离罐IV内进行气液分离，液态丙烷制冷剂经节流阀V节流降温降压后进入预冷换热器进行制冷，变为过热状态进入压缩机III，压缩至过热状态后进入缓冲罐，分离罐IV分离出的气态丙烷制冷剂等压、焓增分离，然后进入缓冲罐，两股丙烷制冷剂在缓冲罐中混合，返回压缩机II，循环完成。
所述的压缩机III内的丙烷制冷剂经过止回阀，然后进入缓冲罐，防止压缩机III排气压力不稳的造成回吸现象。
所述的分离罐IV分离出的气态丙烷制冷剂经过温度控制阀后进入缓冲罐，压缩机II出口温度控制温度控制阀的开闭。
还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I，混合制冷剂被压缩机I压缩后变为高温高压蒸汽状态，经冷却器I后变为常温高压气态，经预冷换热器降温后，混合制冷剂内低沸点产物冷凝，进入分离罐I中进行气液分离，液相混合制冷剂经中冷换热器冷却变为低温度的高压状态，经节流阀II进入分离罐II进行气液分离，分离罐I中气相混合制冷剂经中冷换热器、深冷换热器后，经过节流阀III变为低温低压状态，进入深冷换热器进行制冷，然后进入分离罐III进行气液分离，分离罐II和分离罐III中的液相混合制冷剂合并混合后，经过中冷换热器、预冷换热器进行制冷，分离罐II和分离罐III中的气相混合制冷剂合并混合后，与来自中冷换热器、预冷换热器制冷后的混合制冷剂合并混合，最后进入压缩机I。
所述的天然气液化模块包括液化管，气态天然气通过液化管流经预冷换热器、中冷换热器和中冷换热器制冷吸收冷量，变为液化天然气，然后与节流阀I连通。
所述压缩机I压比在5以下，且混合制冷剂进压缩机无液相。
所述预冷换热器、中冷换热器、深冷换热器换热温差不小于3℃。
本发明的优点：结构相对简单，与传统的丙烷预冷混合制冷剂循环相比，添置部件少，功耗降低明显；在压缩机III后添置缓冲罐，可使两股混合冷剂充分混合，防止液相丙烷制冷剂进压缩机；在压缩机后进缓冲罐入口处增加止回阀，降低压缩机排气压力不稳定造成的影响；在缓冲罐出口即压缩机II出口处安装感温包来控制缓冲罐低温冷剂的量，降低冷量的消耗；温度控制阀和止回阀的设置，保证了本***运行时的节能与稳定。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。
图1为本发明结构示意图。
图中：comp-2为压缩机II、cond-2为冷却器II、v4为节流阀IV、sep-4为分离罐IV、v5为节流阀V、comp-3为压缩机III、Tank为缓冲罐、v6为温度控制阀，v7为止回阀；comp-1为压缩机I、cond-1为冷却器I、sep-1为分离罐I、v2为节流阀II，v3为节流阀III，sep-2为分离罐II、sep-3为分离罐III；LNG-100为预冷换热器、LNG-101为中冷换热器、LNG-102为深冷换热器、v1为降压阀。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有付出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
如图1所示，一种多级压缩丙烷预冷天然气液化***，包括丙烷预冷循环模块和天然气液化模块，丙烷预冷循环模块包括压缩机II comp-2，压缩机II comp-2出口与冷却器II cond-2连通，冷却器II cond-2与节流阀IV v4连通，节流阀IV v4与分离罐IV sep-4连通，分离罐IV sep-4一出口与节流阀V v5连通，节流阀V v5经过预冷换热器 LNG-100后与压缩机III comp-3连通，压缩机III comp-3与缓冲罐 tank连通，分离罐IV sep-4另一出口与缓冲罐 tank连通，缓冲罐 tank与压缩机II comp-2进口连通。
所述的压缩机III comp-3与止回阀 v7连通，止回阀v7与缓冲罐 tank连通。
所述的分离罐IV sep-4另一出口与温度控制阀 v6连通，温度控制阀 v6感应压缩机II comp-2出口温度，温度控制阀 v6与缓冲罐 tank连通。
还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I comp-1，压缩机Icomp-1与冷却器I cond-1连通，冷却器I cond-1经过预冷换热器 LNG-100后与分离罐Isep-1连通，分离罐I sep-1一出口经过中冷换热器 LNG-101后与节流阀II v2连通，节流阀II v2与分离罐II sep-2连通，分离罐I sep-1另一出口经过中冷换热器 LNG-101、深冷换热器 LNG-102后与节流阀III v3连通，节流阀III v3经过深冷换热器 LNG-102后与分离罐III sep-3连通，分离罐II sep-2的一出口与分离罐III sep-3的一出口合并，再与分离罐II sep-2的另一出口与分离罐III sep-3的另一出口合并后经过中冷换热器 LNG-101、预冷换热器 LNG-100的部分合并，然后与压缩机I comp-1连通。
所述的天然气液化模块包括液化管，液化管经过预冷换热器LNG-100、中冷换热器LNG-101和深冷换热器 LNG-102后与节流阀I v1连通。
一种多级压缩丙烷预冷天然气液化***的液化方法，包括丙烷预冷循环模块和天然气液化模块，丙烷预冷循环模块包括压缩机II comp-2，丙烷制冷剂经过压缩机II comp-2压缩后过节点26，然后经冷却器II cond-2过节点27冷却至全液态，经节流阀IV v4节流降压降温后过节点28变为气液两相，在分离罐IV sep-4内进行气液分离，液态丙烷制冷剂过节点29，经节流阀V v5节流降温降压后过节点31，然后进入预冷换热器 LNG-100进行制冷，变为过热状态过节点32后进入压缩机III comp-3，压缩至过热状态后过节点33经过止回阀v7，然后进入缓冲罐tank，止回阀 v7防止压缩机III comp-3排气压力不稳的造成回吸现象，分离罐IV sep-4分离出的气态丙烷制冷剂等压、焓增分离，然后过节点30经过温度控制阀 v6，压缩机II comp-2出口节点26的温度控制温度控制阀 v6的开闭，温度控制阀 v6过节点34后进入缓冲罐 tank，两股丙烷制冷剂在缓冲罐 tank中混合，过节点35后返回压缩机II comp-2，循环完成。
还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I comp-1，混合制冷剂被压缩机I comp-1压缩后过节点5变为高温高压蒸汽状态，经冷却器I cond-1后过节点6变为常温高压气态，过节点7经预冷换热器 LNG-100降温后，过节点8混合制冷剂内低沸点产物冷凝，进入分离罐I sep-1中进行气液分离，液相混合制冷剂过节点10经中冷换热器LNG-101冷却变为低温度的高压状态，过节点11经节流阀II v2进入分离罐II sep-2进行气液分离，分离罐I sep-1中气相混合制冷剂过节点9经中冷换热器 LNG-101，然后过节点15经深冷换热器LNG-102，过节点16经过节流阀III v3变为低温低压状态，过节点17进入深冷换热器 LNG-102进行制冷，然后过节点18进入分离罐III sep-3进行气液分离，分离罐IIsep-2中的液相混合制冷剂过节点13后，与分离罐III sep-3中过节点14的液相混合制冷剂合并混合，然后过节点21经过中冷换热器 LNG-101，过节点23经预冷换热器 LNG-100进行制冷，分离罐II sep-2中的气相混合制冷剂过节点20后，与分离罐III sep-3中过节点19的气相混合制冷剂合并混合，然后经过节点22与来自中冷换热器LNG-101、预冷换热器 LNG-100制冷后，经过节点24的混合制冷剂合并混合，最后过节点25进入压缩机I。
所述的天然气液化模块包括液化管，气态天然气通过液化管流经预冷换热器LNG-100后过节点1，然后流经中冷换热器LNG-101过节点2，再流经中冷换热器LNG-102过节点3，进行制冷吸收冷量，最后流经节流阀I v1过节点4，变为液化天然气。
所述压缩机I comp-1压比在5以下，且混合制冷剂进压缩机I comp-1无液相。
所述预冷换热器LNG-100、中冷换热器LNG-101、深冷换热器LNG-102换热温差不小于3℃。
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (8)

1.一种多级压缩丙烷预冷天然气液化***，包括丙烷预冷循环模块和天然气液化模块，其特征在于：所述的丙烷预冷循环模块包括压缩机II，压缩机II出口与冷却器II连通，冷却器II与节流阀IV连通，节流阀IV与分离罐IV连通，分离罐IV一出口与节流阀V连通，节流阀V经过预冷换热器后与压缩机III连通，压缩机III与缓冲罐连通，分离罐IV另一出口与缓冲罐连通，缓冲罐与压缩机II进口连通；
所述的分离罐IV另一出口与温度控制阀连通，温度控制阀感应压缩机II出口温度，温度控制阀与缓冲罐连通。
2.根据权利要求1所述的多级压缩丙烷预冷天然气液化***，其特征在于：所述的压缩机III与止回阀连通，止回阀与缓冲罐连通。
3.根据权利要求1所述的多级压缩丙烷预冷天然气液化***，其特征在于：还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I，压缩机I与冷却器I连通，冷却器I经过预冷换热器后与分离罐I连通，分离罐I一出口经过中冷换热器后与节流阀II连通，节流阀II与分离罐II连通，分离罐I另一出口经过中冷换热器、深冷换热器后与节流阀III连通，节流阀III经过深冷换热器后与分离罐III连通，分离罐II的一出口与分离罐III的一出口合并，再与分离罐II的另一出口与分离罐III的另一出口合并后经过中冷换热器、预冷换热器的部分合并，然后与压缩机I连通。
4.根据权利要求1所述的多级压缩丙烷预冷天然气液化***，其特征在于：所述的天然气液化模块包括液化管，液化管经过预冷换热器、中冷换热器和深冷换热器后与节流阀I连通。
5.一种多级压缩丙烷预冷天然气液化***的液化方法，包括丙烷预冷循环模块和天然气液化模块，其特征在于：所述的丙烷预冷循环模块包括压缩机II，丙烷制冷剂经过压缩机II压缩后，经冷却器II冷却至全液态，经节流阀IV节流降压降温后变为气液两相，在分离罐IV内进行气液分离，液态丙烷制冷剂经节流阀V节流降温降压后进入预冷换热器进行制冷，变为过热状态进入压缩机III，压缩至过热状态后进入缓冲罐，分离罐IV分离出的气态丙烷制冷剂等压、焓增分离，然后进入缓冲罐，两股丙烷制冷剂在缓冲罐中混合，返回压缩机II，循环完成；
所述的分离罐IV分离出的气态丙烷制冷剂经过温度控制阀后进入缓冲罐，压缩机II出口温度控制温度控制阀的开闭。
6.根据权利要求5所述的多级压缩丙烷预冷天然气液化***的液化方法，其特征在于：所述的压缩机III内的丙烷制冷剂经过止回阀，然后进入缓冲罐，防止压缩机III排气压力不稳的造成回吸现象。
7.根据权利要求5所述的多级压缩丙烷预冷天然气液化***的液化方法，其特征在于：还包括混合制冷剂循环模块，混合制冷剂循环模块包括压缩机I，混合制冷剂被压缩机I压缩后变为高温高压蒸汽状态，经冷却器I后变为常温高压气态，经预冷换热器降温后，混合制冷剂内低沸点产物冷凝，进入分离罐I中进行气液分离，液相混合制冷剂经中冷换热器冷却变为低温度的高压状态，经节流阀II进入分离罐II进行气液分离，分离罐I中气相混合制冷剂经中冷换热器、深冷换热器后，经过节流阀III变为低温低压状态，进入深冷换热器进行制冷，然后进入分离罐III进行气液分离，分离罐II和分离罐III中的液相混合制冷剂合并混合后，经过中冷换热器、预冷换热器进行制冷，分离罐II和分离罐III中的气相混合制冷剂合并混合后，与来自中冷换热器、预冷换热器制冷后的混合制冷剂合并混合，最后进入压缩机I。
8.根据权利要求5所述的多级压缩丙烷预冷天然气液化***的液化方法，其特征在于：所述的天然气液化模块包括液化管，气态天然气通过液化管流经预冷换热器、中冷换热器和中冷换热器制冷吸收冷量，变为液化天然气，然后与节流阀I连通。
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