CN217465150U - 一种适合高含二氧化碳天然气的乙烷回收装置 - Google Patents

一种适合高含二氧化碳天然气的乙烷回收装置 Download PDF

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CN217465150U
CN217465150U CN202221351532.6U CN202221351532U CN217465150U CN 217465150 U CN217465150 U CN 217465150U CN 202221351532 U CN202221351532 U CN 202221351532U CN 217465150 U CN217465150 U CN 217465150U
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heat exchanger
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demethanizer
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carbon dioxide
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冷南江
马国光
雷洋
张涛
彭豪
熊祚帅
陈玉婷
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Southwest Petroleum University
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Abstract

本实用新型涉及一种适合高含二氧化碳天然气的乙烷回收装置，包括：预冷换热器、主换热器、过冷换热器、预分离器、低温分离器、膨胀机组膨胀端、膨胀机组增压端、外输气压缩机、第一空冷器、第二空冷器、脱甲烷塔。在部分干气循环工艺的基础上，利用丙烷及以上的液烃对二氧化碳的溶解吸收作用，采用预冷分离出部分脱水干气液相与外输干气回流混合冷却后再与低温分离器分离出的部分气相与部分液相混合过冷进入脱甲烷塔顶部，增加脱甲烷塔顶部的丙烷及以上的液烃含量，提高塔顶的二氧化碳冻堵裕量。所述方法采用多级制冷、多级分离以及多次气相与液相混合，提高了天然气乙烷回收装置对二氧化碳的适应性，能够有效控制二氧化碳固体的形成。

Description

一种适合高含二氧化碳天然气的乙烷回收装置
技术领域
本实用新型涉及天然气处理加工技术领域，具体为一种高含二氧化碳天然气的乙烷回收装置。
背景技术
对天然气进行乙烷回收能增强对天然气资源的合理利用，并且在近年来，各大油气田已经将其视为了新的效益增长点。然而，由于二氧化碳驱采油技术的应用，导致天然气中二氧化碳含量较高，成为了乙烷回收深冷装置正常生产的障碍，高含量的二氧化碳极易在脱甲烷塔的上部发生冻堵现象，不仅会导致乙烷回收率降低，还会影响安全生产。
现有的典型乙烷回收流程如附图2所示，它的特点是将低温分离器气相或气相与液相的混合相与脱甲烷塔顶气相换热过冷后调压进入脱甲烷塔的中上部，其作用为既可以增加塔中上部的低温位冷量，还能增加液烃含量吸收气相中的二氧化碳与乙烷，实现降低二氧化碳冻堵风险与提高乙烷回收率。当脱水干气中二氧化碳含量升高时，需要增加外输干气的回流量维持较高乙烷回收率，同时还需要增加低温分离器的过冷液相流量，以期提升脱甲烷塔的二氧化碳冻堵裕量，这些操作会导致装置的乙烷回收率降低，能耗也会急剧上升。
为了克服上述典型乙烷回收流程对脱水干气中的二氧化碳适应性不高，并降低装置能耗，本实用新型开发了一种高含二氧化碳天然气的乙烷回收装置，利用丙烷及以上的液烃对二氧化碳的溶解吸收能力，增加脱甲烷塔顶部的丙烷及以上的液烃量，降低塔顶气相中的二氧化碳含量，提升塔顶的二氧化碳冻堵裕量。
发明内容
本实用新型的目的是为了解决上述问题而提供一种高含二氧化碳天然气的乙烷回收装置。
本实用新型通过以下技术方案来实现上述目的：
本实用新型提供一种高含二氧化碳天然气的乙烷回收装置，该方法在低温分离工艺中利用丙烷及以上的液烃对二氧化碳的溶解吸收作用，采用预冷分离出部分脱水干气液相与外输干气回流混合冷却后再与低温分离器分离出的部分气相与部分液相混合过冷进入脱甲烷塔顶部，增加脱甲烷塔顶部的丙烷及以上的液烃含量，提高塔顶的二氧化碳冻堵裕量。
本实用新型提供的技术方案：
包括预冷换热器、主换热器、过冷换热器、预分离器、低温分离器、膨胀机组膨胀端、膨胀机组增压端、外输气压缩机、第一空冷器、第二空冷器、脱甲烷塔；
脱水干气进入预冷换热器换热后进入预分离器分离出气相和液相，预分离器分离出的气相经主换热器冷却后进入低温分离器分离出气相和液相，低温分离器分离出的部分气相经膨胀机组膨胀端降压降温后进入脱甲烷塔上部，分离出的部分液相经调压后进入脱甲烷塔中部；预分离器分离出的液相与经过预冷换热器预冷后的外输干气回流混合后进入主换热器换热，然后与低温分离器分离出的部分气相与部分液相混合后进入过冷换热器过冷，经调压后进入脱甲烷塔顶部。
脱甲烷塔塔顶出来的气相依次经过过冷换热器、主换热器和预冷换热器换热升温后进入膨胀机组增压端增压、第一空冷器降温、外输气压缩机增压和第二空冷器降温后外输；
脱甲烷塔塔底出来的液相去向脱乙烷塔。
进一步的技术方案，外输干气回流经预冷换热器换热降温后与预分离器分离出的液相混合，混合相经主换热器换热降温后再与来自低温分离器分离出的部分气相与部分液相混合，进入过冷换热器换热过冷并经调压后进入脱甲烷塔顶部。
进一步的技术方案，所述外输干气回流比例为外输干气总流量的10％～20％。
进一步的技术方案，所述低温分离器分离出的部分气相占低温分离器气相的10％～30％，分离出的部分液相占低温分离器液相的10％～90％。
进一步的技术方案，所述预冷换热器、主换热器和过冷换热器的类型均为多股流板翅式换热器，将两股热流与三股冷流、两股热流与四股冷流、一股热流与一股冷流分别集成于预冷换热器、主换热器和过冷换热器中。
进一步的技术方案，所述预冷换热器中的两股热流分别为脱水干气与外输干气回流，三股冷流分别为经过冷换热器、主换热器换热后的脱甲烷塔塔顶出来的气相、脱甲烷塔塔底的侧线抽出物流与外加冷剂；所述主换热器中的两股热流分别为预分离器分离出气相以及预分离器分离出液相与经预冷换热器换热后的外输干气回流的混合相，四股冷流分别为经过冷换热器换热后的脱甲烷塔塔顶出来的气相、两股脱甲烷塔中部的侧线抽出物流与外加冷剂；所述过冷换热器中的一股热流为预分离器分离出的液相与外输干气回流混合进入主换热器换热后与低温分离器分离出的部分气相与部分液相的混合相，一股冷流为脱甲烷塔塔顶出来的气相。采用上述技术方案所产生的有益效果：
本实用新型采用多级制冷、多级分离以及多次气相与液相混合，降低了脱甲烷塔顶部的二氧化碳含量，提高了二氧化碳冻堵裕量。在相同条件下与典型乙烷回收工艺相比，本实用新型在维持高乙烷回收率的同时，装置能适应的脱水干气二氧化碳含量提升到了1.8％，有效降低了二氧化碳冻堵风险。本实用新型脱甲烷塔设置了多股侧线采出进入换热器释放冷量，提升了热集成度，提高了能量利用率，降低了装置的系统能耗。
附图说明
图1是本实用新型的工艺流程图；
图1中所示：HR101-预冷换热器、HR102-主换热器、HR103-过冷换热器、V101-预分离器、V102-低温分离器、K101-膨胀机组压缩端、K102-膨胀机组膨胀端、K103-外输气压缩机、AC101-第一空冷器、AC-102-第二空冷器、T101-脱甲烷塔。
图2是现有的典型乙烷回收工艺流程图；
图2中所示：HR201-换热器、HR202-过冷换热器、V201-低温分离器、K201-膨胀机组压缩端、K202-膨胀机组膨胀端、K203-外输气压缩机、AC201-第一空冷器、AC-202-第二空冷器、T201-脱甲烷塔。
图3是本实用新型实例1的工艺流程图；
图3中所示：HR301-预冷换热器、HR302-主换热器、HR303-过冷换热器、HR304-冷却器、HR305-脱乙烷塔塔底重沸器、V301-预分离器、V302-低温分离器、V303-脱乙烷塔塔顶回流罐、K301-膨胀机组压缩端、K302-膨胀机组膨胀端、K303-外输气压缩机、AC301-第一空冷器、AC-302-第二空冷器、T301-脱甲烷塔、T302-脱乙烷塔、P301-脱甲烷塔塔底增压泵、P302-脱乙烷塔塔顶回流泵。
具体实施方式
下面结合实施例中的附图3对本实用新型中的技术方案做进一步说明。
实施例1
本实用新型的实施例1如图3所示，脱水干气气质组成及工况如下：
脱水干气处理规模：600×104m3/d
脱水干气压力：5.5MPa
脱水干气温度：25℃
外输干气压力：5MPa
脱水干气组成如表1所示。
表1脱水干气气质组成
组分 N<sub>2</sub> CO<sub>2</sub> C<sub>1</sub> C<sub>2</sub> C<sub>3</sub>
mol％ 0.5331 0.9664 87.9573 6.6051 2.6178
组分 iC<sub>4</sub> nC<sub>4</sub> iC<sub>5</sub> nC<sub>5</sub> nC<sub>6</sub>
mol％ 0.5997 0.0543 0.1142 0.2570 0.2951
如图3所示，本实用新型公开了一种适合高含二氧化碳天然气的乙烷回收装置，进乙烷回收装置的脱水干气(5.5MPa、25℃)进入预冷换热器HR301换热(5.45MPa、-25℃)后进入预分离器V301分离出气相和液相，预分离器V301分离出的气相经主换热器HR302冷却(5.4MPa、-47℃)后进入低温分离器V302分离出气相和液相，低温分离器V302分离出的部分气相(其流量占低温分离器V302气相总流量的79％)经膨胀机组膨胀端K302降压降温(2.0MPa、-85.7℃)后进入脱甲烷塔T301上部，分离出的部分液相(其流量占低温分离器V302液相总流量的81％)经调压(2.0MPa、-72.69℃)后进入脱甲烷塔T301中部；预分离器V301分离出的液相与经过预冷换热器HR301预冷后的外输干气回流(其流量占外输干气总流量的13％)混合后进入主换热器HR302换热(4.9MPa、-60℃)，然后与低温分离器V302分离出的部分气相(其流量占低温分离器V302气相总流量的21％)与部分液相(其流量占低温分离器V302液相总流量的19％)混合后进入过冷换热器HR303过冷后经调压(2.0MPa、-104℃)进入脱甲烷塔T301顶部。
脱甲烷塔T301塔顶出来的气相依次经过过冷换热器HR303、主换热器HR302和预冷换热器HR301换热升温(1.75MPa、24℃)后进入膨胀机组增压端K301增压(2.16MPa、43.78℃)，再经第一空冷器AC301降温后进入外输气压缩机K303增压至5.0MPa最后经第二空冷器AC302降温至30℃后外输，外输干气总流量为538×104m3/d。
从脱甲烷塔中下部采出两股低温物流(-82.93℃，-69.47℃)作侧线重沸，均进入主换热器HR302换热升温(-63.4℃、-49.3℃)后回流入脱甲烷塔T301。从脱甲烷塔T301塔底采出一股低温物流(-6.1℃)进入预冷换热器HR301换热升温至5.2℃后回流入脱甲烷塔T301。外加冷剂制冷系统采用混合冷剂，其中丙烷占比60％，乙烯占比40％，总循环量98540kg/h，分别为预冷换热器HR301提供-31℃的温位，为主换热器HR302提供-54℃的温位。
脱甲烷塔T301塔底出来的液相(2.0MPa、10.47℃)经泵P301增压至2.5MPa后进入脱乙烷塔T301，脱乙烷塔T301塔顶出来的气相分为两部分，一部分作为乙烷产品(其流量占脱乙烷塔T301塔顶气相总流量的50％)外输，流量为46.29×104m3/d，另一部分经冷却器HR304降温(4.03℃)后进入脱乙烷塔T302塔顶回流罐V303分离气液相，分离出的液相经回流泵P302增压至2.5MPa后回流进入脱乙烷塔T302塔顶。
脱乙烷塔T302塔底出来的液相(2.45MPa、98.05℃)为含丙烷及以上重组分的凝液，其中乙烷摩尔含量为1％，凝液总流量为16350kg/h。其乙烷回收装置的乙烷回收率为93.8％。本实施例方案与现有典型乙烷回收流程相比，本实用新型提出的一种适合高含二氧化碳天然气的乙烷回收装置，脱甲烷塔二氧化碳冻堵裕量控制在5℃以上，乙烷回收率提高2.7％，有效降低了二氧化碳冻堵风险，提高了装置的经济效益。
以上所述，通过实施例揭示本实用新型内容，但是并非用以限定本实用新型，本行业内的技术人员应了解，在不脱离本实用新型技术方案范围内，利用上述的技术内容做出变动或修饰应视为同等的实施例。所有未脱离本实用新型技术方案，依据本实用新型的说明内容做出的所有简单修改、等同变化与修饰，均包括在本技术方案范围内。本实用新型要求保护范围由所提出的权利要求书及具有同效应的内容进行界定。

Claims (6)

1.一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于：
包括预冷换热器(HR101)、主换热器(HR102)、过冷换热器(HR103)、预分离器(V101)、低温分离器(V102)、膨胀机组增压端(K101)、膨胀机组膨胀端(K102)、外输气压缩机(K103)、第一空冷器(AC101)、第二空冷器(AC102)、脱甲烷塔(T101)；
脱水干气进入预冷换热器(HR101)换热后进入预分离器(V101)分离出气相和液相，预分离器(V101)分离出的气相经主换热器(HR102)冷却后进入低温分离器(V102)分离出气相和液相，低温分离器(V102)分离出的部分气相经膨胀机组膨胀端(K102)降压降温后进入脱甲烷塔(T101)上部，分离出的部分液相经调压后进入脱甲烷塔(T101)中部；预分离器(V101)分离出的液相与经过预冷换热器(HR101)预冷后的外输干气回流混合后进入主换热器(HR102)换热，然后与低温分离器(V102)分离出的部分气相与液相混合后进入过冷换热器(HR103)过冷，经调压后进入脱甲烷塔(T101)顶部；
脱甲烷塔(T101)塔顶出来的气相依次经过过冷换热器(HR103)、主换热器(HR102)和预冷换热器(HR101)换热升温后进入膨胀机组增压端(K101)增压、第一空冷器(AC101)降温、外输气压缩机(K103)增压、第二空冷器(AC102)降温后外输；
脱甲烷塔(T101)塔底出来的液相去向脱乙烷塔。
2.根据权利要求1所述的一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于，外输干气回流经预冷换热器(HR101)换热降温后与预分离器(V101)分离出的液相混合，混合相经主换热器(HR102)换热降温后再与来自低温分离器(V102)分离出的部分气相与液相混合，进入过冷换热器(HR103)换热过冷并经调压后进入脱甲烷塔(T101)顶部。
3.根据权利要求2所述的一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于，所述外输干气回流比例为外输干气总流量的10％～20％。
4.根据权利要求2所述的一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于，所述低温分离器(V102)分离出的部分气相占低温分离器气相的10％～30％，分离出的部分液相占低温分离器液相的10％～90％。
5.根据权利要求1所述的一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于，所述预冷换热器(HR101)、主换热器(HR102)和过冷换热器(HR103)的类型均为多股流板翅式换热器，将两股热流与三股冷流、两股热流与四股冷流、一股热流与一股冷流分别集成于预冷换热器(HR101)、主换热器(HR102)和过冷换热器(HR103)中。
6.根据权利要求5所述的一种适合高含二氧化碳天然气的乙烷回收装置，其特征在于，所述预冷换热器(HR101)中的两股热流分别为脱水干气与外输干气回流，三股冷流分别为经过冷换热器(HR103)、主换热器(HR102)换热后的脱甲烷塔(T101)塔顶出来的气相、脱甲烷塔(T101)塔底的侧线抽出物流与外加冷剂；所述主换热器(HR102)中的两股热流分别为预分离器(V101)分离出气相以及预分离器(V101)分离出液相与经预冷换热器(HR101)换热后的外输干气回流的混合相，四股冷流分别为经过冷换热器(HR103)换热后的脱甲烷塔(T101)塔顶出来的气相、两股脱甲烷塔(T101)中部的侧线抽出物流与外加冷剂；所述过冷换热器(HR103)中的一股热流为预分离器(V101)分离出的液相与外输干气回流混合进入主换热器(HR102)换热后与低温分离器(V102)分离出的部分气相与部分液相的混合相，一股冷流为脱甲烷塔(T101)塔顶出来的气相。
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* Cited by examiner, † Cited by third party
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