CN111849573A - 一种轻烃回收系统 - Google Patents

一种轻烃回收系统 Download PDF

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CN111849573A
CN111849573A CN201910344764.5A CN201910344764A CN111849573A CN 111849573 A CN111849573 A CN 111849573A CN 201910344764 A CN201910344764 A CN 201910344764A CN 111849573 A CN111849573 A CN 111849573A
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gas
liquid separator
stage
cooling device
deethanizer
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丁垚
郑友林
李奇
邱伟伟
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China Petroleum and Chemical Corp
Sinopec Exploration and Production Research Institute
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China Petroleum and Chemical Corp
Sinopec Exploration and Production Research Institute
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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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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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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Abstract

本发明提供一种轻烃回收系统，包括一级气液分离器、一级压缩机、一级冷却装置、二级气液分离器、二级压缩机、二级冷却装置、三级气液分离器、脱乙烷塔和脱丙烷塔。其中，一级气液分离器与一级压缩机连接，一级冷却装置与一级压缩机连接、二级气液分离器与一级冷却装置连接，二级压缩机与二级气液分离器连接，二级冷却装置与二级压缩机连接，三级气液分离器与二级冷却装置连接。一级气液分离器、二级气液分离器和三级气液分离器均与脱乙烷塔连接，脱乙烷塔与脱丙烷塔连接。脱乙烷塔的塔顶气出口与二级气液分离器的入口连接。本发明提供的轻烃回收系统能够提高轻烃回收率。

Description

一种轻烃回收系统
技术领域
本发明涉及天然气中轻烃回收处理技术领域，具体涉及一种轻烃回收系统。
背景技术
天然气中除含有甲烷外，还含有一定量的乙烷、丙烷、丁烷、戊烷以及更重烃类。为了符合商品天然气质量指标或管输气对烃露点的质量要求，或为了获得宝贵的液体燃料和化工原料，需将天然气中的烃类按照一定要求分离与回收。从天然气中回收凝液的工艺过程称之为天然气凝液回收，我国习惯上称为轻烃回收。回收到的天然气凝液或直接作为商品，或根据有关产品质量指标进一步分离为乙烷、液化石油气及天然汽油等产品。天然气凝液回收是一个十分重要的工艺过程，它取决于天然气的类型和数量、天然气凝液回收目的、方法及产品价格等，特别是取决于哪些可以回收的烃类组分是作为液体产品还是作为商品气中组分时的经济效益比较。现有技术中的轻烃回收工艺装置，由于有相当一部分丙烷从低温分离器、脱乙烷塔顶馏出进入干气中，因此存在轻烃回收率较低的问题。
发明内容
本发明要解决的技术问题是克服现有技术的不足，提供一种能够提高轻烃回收率的轻烃回收装置。
为解决上述技术问题，本发明提出的技术方案为：
一种轻烃回收系统，包括一级气液分离器、一级压缩机、一级冷却装置、二级气液分离器、二级压缩机、二级冷却装置、三级气液分离器、脱乙烷塔和脱丙烷塔。其中，一级气液分离器与一级压缩机连接，一级冷却装置与一级压缩机连接、二级气液分离器与一级冷却装置连接，二级压缩机与二级气液分离器连接，二级冷却装置与二级压缩机连接，三级气液分离器与二级冷却装置连接。一级气液分离器、二级气液分离器和三级气液分离器均与脱乙烷塔连接，脱乙烷塔与脱丙烷塔连接。脱乙烷塔的塔顶气出口与二级气液分离器的入口连接。
根据本发明的轻烃回收系统，原料气先在一级分离器中除去游离的油、水、和其他杂质，然后经过一级压缩机增压，增压后的原料气通过一级冷却系统降温后进入二级分离器进行气、液分离。分离出来的干气主要组分时甲烷、乙烷及少量丙烷，凝液主要是组分是C3+烃类和少部分的甲烷和乙烷。各级分离器分离出来的各级凝液进入脱乙烷塔脱除甲烷及乙烷，塔底油进入脱丙烷塔。从脱丙烷塔塔顶脱除的丙烷、丁烷即为油气田液化石油气，塔底则为稳定后的轻烃。由于脱乙烷塔的塔顶气出口回接到二级气液分离器入口，因此，从脱乙烷塔脱除乙烷后的塔顶气能够与原料气共同经过二级压缩机进入制冷系统以及三级气液分离器，再次获取冷量进行轻烃回收，从而进一步脱除干气中的丙烷等轻烃，提高稳定轻烃的回收率。
对于上述技术方案，还可进行如下所述的进一步地改进。
根据本发明的轻烃回收系统，在一个优选的实施方式中，一级冷却装置包括水冷装置和冷剂蒸发器，水冷装置分别与一级压缩机和冷剂蒸发器连接，冷剂蒸发器与二级分离器连接。
水冷装置能够使得增压后的原料气冷却至常温，再经过冷剂蒸发器冷冻降温，从而便于二级分离器进行分离。
进一步地，在一个优选的实施方式中，一级冷却装置还包括空冷装置，空冷装置分别与水冷装置和冷剂蒸发器连接。
通过设置空冷装置的气/气换热，能够对从水冷装置出来的原料气预冷后进入冷剂蒸发器，从而减少冷剂蒸发器的负担和降低成本。
具体地，在一个优选的实施方式中，二级气液分离装置为低温分离器。
二级气液分离器设置成低温分离器，有利于提高气液分离的效果。
进一步地，在一个优选的实施方式中，根据本发明的轻烃回收系统，还包括三级冷却装置和四级气液分离器。三级冷却装置分别与三级气液分离器和四级气液分离器连接。
通过设置多级冷却装置和多级分离器，有利于进一步脱除干气中的丙烷等轻烃，提高稳定轻烃回收率。
具体地，在一个优选的实施方式中，脱乙烷塔的塔顶气出口与第一冷却装置连接，第一冷却装置与第一气液分离器连接，第一气液分离器的顶部出口与二级气液分离器连接，第一气液分离器的底部出口与二脱乙烷塔连接。
通过冷却装置和气液分离器对塔顶气再次分离的结构形式，有利于提高脱除甲烷、乙烷的效率。
进一步地，在一个优选的实施方式中，脱乙烷塔的底部出口与第二冷却装置连接，第二冷却装置与第二气液分离器连接，第二气液分离器的顶部出口与脱乙烷塔连接，第二气液分离器的底部出口与脱丙烷塔连接。
通过冷却装置和气液分离器对塔底凝液再次分离的结构形式，有利于提高脱除甲烷、乙烷的效率。
进一步地，在一个优选的实施方式中，脱丙烷塔的塔顶气出口与第三冷却装置连接，第三冷却装置与第三气液分离器连接，第三气液分离器的底部出口与脱丙烷塔连接。
通过冷却装置和气液分离器对塔顶气再次分离的结构形式，有利于提高脱除丙烷、丁烷的效率。
进一步地，在一个优选的实施方式中，脱丙烷塔的底部出口与第四冷却装置连接，第四冷却装置与第四气液分离器连接，第四气液分离器的顶部出口与脱丙烷塔连接。
通过冷却装置和气液分离器对塔底凝液再次分离的结构形式，有利于提高脱除丙烷、丁烷的效率。
具体地，在一个优选的实施方式中，一级气液分离器、二级气液分离器和三级气液分离器的底部出口分别与脱乙烷塔连接。
具体地，在另一个优选的实施方式中，一级气液分离器、二级气液分离器和三级气液分离器的底部出口通过管道互相连接之后与脱乙烷塔连接。
与现有技术相比，本发明的优点在于：能够提高轻烃回收率。
附图说明
在下文中将基于实施例并参考附图来对本发明进行更详细的描述。其中：
图1示意性显示了本发明实施例的轻烃回收系统的整体结构；
图2示意性显示了本发明实施例的轻烃回收系统的另一整体结构。
在附图中，相同的部件使用相同的附图标记。附图并未按照实际的比例绘制。
具体实施方式
下面将结合附图和具体实施例对本发明作进一步详细说明，但并不因此而限制本发明的保护范围。
图1示意性显示了本发明实施例的轻烃回收系统10的整体结构。图2示意性显示了本发明实施例的轻烃回收系统10的另一整体结构。
如图1和图2所示，本发明实施例的轻烃回收系统10，包括一级气液分离器1、一级压缩机2、一级冷却装置3、二级气液分离器4、二级压缩机5、二级冷却装置6、三级气液分离器7、脱乙烷塔8和脱丙烷塔9。其中，一级气液分离器1与一级压缩机2连接，一级冷却装置3与一级压缩机2连接、二级气液分离器4与一级冷却装置3连接，二级压缩机5与二级气液分离器4连接，二级冷却装置6与二级压缩机5连接，三级气液分离器7与二级冷却装置6连接。一级气液分离器1、二级气液分离器4和三级气液分离器7均与脱乙烷塔8连接，脱乙烷塔8与脱丙烷塔9连接。脱乙烷塔8的塔顶气出口与二级气液分离器4的入口连接。
根据本发明实施例的轻烃回收系统，原料气先在一级分离器中除去游离的油、水、和其他杂质，然后经过一级压缩机增压，增压后的原料气通过一级冷却系统降温后进入二级分离器进行气、液分离。分离出来的干气主要组分时甲烷、乙烷及少量丙烷，凝液主要是组分是C3+烃类和少部分的甲烷和乙烷。各级分离器分离出来的各级凝液进入脱乙烷塔脱除甲烷及乙烷，塔底油进入脱丙烷塔。从脱丙烷塔塔顶脱除的丙烷、丁烷即为油气田液化石油气，塔底则为稳定后的轻烃。由于脱乙烷塔的塔顶气出口回接到二级气液分离器入口，因此，从脱乙烷塔脱除乙烷后的塔顶气能够与原料气共同经过二级压缩机进入制冷系统以及三级气液分离器，再次获取冷量进行轻烃回收，从而进一步脱除干气中的丙烷等轻烃，提高稳定轻烃的回收率。
具体地，如图1所示，在一个优选的实施方式中，一级气液分离器1、二级气液分离器4和三级气液分离器7的底部出口分别与脱乙烷塔8连接。具体地，如图2所示，在另一个优选的实施方式中，一级气液分离器1、二级气液分离器4和三级气液分离器7的底部出口通过管道互相连接之后与脱乙烷塔8连接。具体地，在一个优选的实施方式中，二级气液分离器4为低温分离器。二级气液分离器设置成低温分离器，有利于提高气液分离的效果。
优选地，根据本发明实施例的轻烃回收系统10，还包括三级冷却装置101和四级气液分离器102。三级冷却装置101分别与三级气液分离器7和四级气液分离器102连接。通过设置多级冷却装置和多级分离器，有利于进一步脱除干气中的丙烷等轻烃，提高稳定轻烃回收率。
如图1和图2所示，根据本发明实施例的轻烃回收系统10，优选地，在本实施例中，一级冷却装置3包括水冷装置和冷剂蒸发器，水冷装置分别与一级压缩机和冷剂蒸发器连接，冷剂蒸发器与二级分离器4连接。水冷装置能够使得增压后的原料气冷却至常温，再经过冷剂蒸发器冷冻降温，从而便于二级分离器进行分离。进一步地，在本实施例中，一级冷却装置3还包括空冷装置，空冷装置分别与水冷装置和冷剂蒸发器连接。通过设置空冷装置的气/气换热，能够对从水冷装置出来的原料气预冷后进入冷剂蒸发器，从而减少冷剂蒸发器的负担和降低成本。
具体地，如图1和图2所示，在一个优选的实施方式中，脱乙烷塔8的塔顶气出口与第一冷却装置81连接，第一冷却装置81与第一气液分离器82连接，第一气液分离器82的顶部出口与二级气液分离器4连接，第一气液分离器82的底部出口与二脱乙烷塔8连接。通过冷却装置和气液分离器对塔顶气再次分离的结构形式，有利于提高脱除甲烷、乙烷的效率。进一步地，在一个优选的实施方式中，脱乙烷塔8的底部出口与第二冷却装置83连接，第二冷却装置83与第二气液分离器84连接，第二气液分离器84的顶部出口与脱乙烷塔8连接，第二气液分离器84的底部出口与脱丙烷塔9连接。通过冷却装置和气液分离器对塔底凝液再次分离的结构形式，有利于提高脱除甲烷、乙烷的效率。
进一步地，如图1和图2所示，在本实施例中，脱丙烷塔9的塔顶气出口与第三冷却装置91连接，第三冷却装置91与第三气液分离器92连接，第三气液分离器91的底部出口与脱丙烷塔9连接。通过冷却装置和气液分离器对塔顶气再次分离的结构形式，有利于提高脱除丙烷、丁烷的效率。进一步地，在本实施例中，脱丙烷塔9的底部出口与第四冷却装置93连接，第四冷却装置93与第四气液分离器94连接，第四气液分离器94的顶部出口与脱丙烷塔9连接。通过冷却装置和气液分离器对塔底凝液再次分离的结构形式，有利于提高脱除丙烷、丁烷的效率。
利用Hysys软件模拟本发明实施例的轻烃回收系统，经过模拟计算得出，轻烃回收率至少提高了8.87％。
根据上述实施例，可见，本发明涉及的轻烃回收系统，能够提高轻烃回收率。
虽然已经参考优选实施例对本发明进行了描述，但在不脱离本发明范围的情况下，可以对其进行各种改进并且可以用等效物替换其中的部件。尤其是，只要不存在结构冲突，各个实施例中所提到的各项技术特征均可以任意方式组合起来。本发明并不局限于文中公开的特定实施例，而是包括落入权利要求范围内的所有技术方案。

Claims (10)

1.一种轻烃回收系统，其特征在于，包括一级气液分离器、一级压缩机、一级冷却装置、二级气液分离器、二级压缩机、二级冷却装置、三级气液分离器、脱乙烷塔和脱丙烷塔；其中，
所述一级气液分离器与所述一级压缩机连接，所述一级冷却装置与所述一级压缩机连接，所述二级气液分离器与所述一级冷却装置连接，所述二级压缩机与所述二级气液分离器连接，所述二级冷却装置与所述二级压缩机连接，所述三级气液分离器与所述二级冷却装置连接；
所述一级气液分离器、所述二级气液分离器和所述三级气液分离器均与所述脱乙烷塔连接，所述脱乙烷塔与所述脱丙烷塔连接；
所述脱乙烷塔的塔顶气出口与所述二级气液分离器的入口连接。
2.根据权利要求1所述的轻烃回收系统，其特征在于，所述一级冷却装置包括水冷装置和冷剂蒸发器，所述水冷装置分别与所述一级压缩机和所述冷剂蒸发器连接，所述冷剂蒸发器与所述二级分离器连接。
3.根据权利要求2所述的轻烃回收系统，其特征在于，所述一级冷却装置还包括空冷装置，所述空冷装置分别与所述水冷装置和所述冷剂蒸发器连接。
4.根据权利要求2或3所述的轻烃回收系统，其特征在于，所述二级气液分离装置为低温分离器。
5.根据权利要求1至4中任一项所述的轻烃回收系统，其特征在于，还包括三级冷却装置和四级气液分离器；所述三级冷却装置分别与所述三级气液分离器和所述四级气液分离器连接。
6.根据权利要求1至5中任一项所述的轻烃回收系统，其特征在于，所述脱乙烷塔的塔顶气出口与第一冷却装置连接，所述第一冷却装置与第一气液分离器连接，所述第一气液分离器的顶部出口与所述二级气液分离器连接，所述第一气液分离器的底部出口与所述二脱乙烷塔连接。
7.根据权利要求6所述的轻烃回收系统，其特征在于，所述脱乙烷塔的底部出口与第二冷却装置连接，所述第二冷却装置与第二气液分离器连接，所述第二气液分离器的顶部出口与所述脱乙烷塔连接，所述第二气液分离器的底部出口与所述脱丙烷塔连接。
8.根据权利要求1至7中任一项所述的轻烃回收系统，其特征在于，所述脱丙烷塔的塔顶气出口与第三冷却装置连接，所述第三冷却装置与第三气液分离器连接，所述第三气液分离器的底部出口与所述脱丙烷塔连接。
9.根据权利要求8所述的轻烃回收系统，其特征在于，所述脱丙烷塔的底部出口与第四冷却装置连接，所述第四冷却装置与第四气液分离器连接，所述第四气液分离器的顶部出口与所述脱丙烷塔连接。
10.根据权利要求1至9中任一项所述的轻烃回收系统，其特征在于，所述一级气液分离器、所述二级气液分离器和所述三级气液分离器的底部出口分别与所述脱乙烷塔连接。
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114854463A (zh) * 2021-02-03 2022-08-05 中国石油天然气股份有限公司 脱水脱烃装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1515651A (zh) * 2003-08-23 2004-07-28 辽河石油勘探局 小型撬装天然气轻烃回收方法
CN203672050U (zh) * 2014-01-21 2014-06-25 李燕 液态天然气回收装置
CN105783421A (zh) * 2016-04-07 2016-07-20 成都赛普瑞兴科技有限公司 一种天然气轻烃回收的方法及装置
CN106316758A (zh) * 2015-06-24 2017-01-11 中石化广州工程有限公司 甲醇转化制丙烯反应产物的分离方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1515651A (zh) * 2003-08-23 2004-07-28 辽河石油勘探局 小型撬装天然气轻烃回收方法
CN203672050U (zh) * 2014-01-21 2014-06-25 李燕 液态天然气回收装置
CN106316758A (zh) * 2015-06-24 2017-01-11 中石化广州工程有限公司 甲醇转化制丙烯反应产物的分离方法
CN105783421A (zh) * 2016-04-07 2016-07-20 成都赛普瑞兴科技有限公司 一种天然气轻烃回收的方法及装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
勘察设计注册工程师石油天然气专业管理委员会: "《勘察设计注册石油天然气工程师资格考试专业考试复习指南》", 31 July 2006 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114854463A (zh) * 2021-02-03 2022-08-05 中国石油天然气股份有限公司 脱水脱烃装置
CN114854463B (zh) * 2021-02-03 2023-05-26 中国石油天然气股份有限公司 脱水脱烃装置

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