CN103822438B - 一种浅冷轻烃回收工艺方法 - Google Patents

一种浅冷轻烃回收工艺方法 Download PDF

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CN103822438B
CN103822438B CN201210464242.7A CN201210464242A CN103822438B CN 103822438 B CN103822438 B CN 103822438B CN 201210464242 A CN201210464242 A CN 201210464242A CN 103822438 B CN103822438 B CN 103822438B
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王勇
王文武
郭亚红
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China Petroleum and Natural Gas Co Ltd
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Abstract

本发明涉及一种浅冷轻烃回收工艺方法，原料气经过分离后，进压缩机压缩，冷却后分离进压缩机增压，增压后在分离出气体和液烃；气体进四股流板翅式换热器第一管程；经过冷却后，经低温分离器进四股板翅式流换热器第二管程，换热后干气外输；液烃经分配器分成二股，一股液烃进四股流板翅式换热器第三管程，循环回分离器；第二股液烃经进四股流板翅式换热器第四管程；换热后进脱乙烷塔；分离器通过液烃泵脱乙烷塔；脱乙烷塔塔顶气体进分离器；脱乙烷塔塔底混烃进液化气塔；液化气塔塔顶外输液化气；液化气塔塔底外输轻油；该方法比常规的浅冷冷凝+冷油吸收法节省能耗63.3％。

Description

一种浅冷轻烃回收工艺方法
技术领域
本发明涉及一种轻烃回收方法，特别是一种伴生气的浅冷回收制冷工艺方法。
背景技术
一般情况下，浅冷轻烃回收工艺是采用冷凝法，或者冷凝+冷油吸收法。其具体工艺流程为：从联合站三相分离器分出的伴生气或者从接转站气液分离器出来的伴生气（温度25℃，压力0.3MPa），经过油气分离器分离出部分凝液后，进入一级压缩机经行压缩，压缩完成后进行分离冷却（温度40℃，压力0.98MPa），然后进入二级压缩机经行压缩冷却(温度40℃，压力2.2MPa），压缩完成后进入丙烷制冷系统，制冷后（温度5℃，压力2.17MPa）进入脱乙烷塔。
通常脱乙烷塔的压力控制在1.7MPa-1.72MPa之间。设定塔顶乙烷的百分比为6％。从塔底出来的混烃（温度79.3℃，压力1.72MPa）先经过液烃换热器换热再（温度83℃，压力1.71MPa）进入液化气塔，塔顶的贫气输至丙烷换热器进行冷却。
液化气塔的压力控制在1.3-1.32MPa之间。设定塔底的温度为150℃，设定塔顶参数（iC5,nC5）的限定含量为3％。经过精馏闪蒸后，塔顶的液化气（40℃,1.28MPa）外输至罐区。塔底的轻油（150℃,1.32MPa）先经过液烃换热器冷却，再经空冷器冷却（温度40℃，压力1.29MPa）后产品分成两部分：一部分作为产品外输至罐区；另一部分经过丙烷换热器冷却后变为冷冻油（-25℃,1.28MPa），进入吸收塔顶部。脱乙烷塔顶出来的贫气经过丙烷蒸发器冷却后（-25℃,1.69MPa）进入吸收塔的底部。
吸收塔压力控制在1.2MPa-1.25MPa，温度控制在-25℃。冷油在吸收塔里经过完全的传质传热，充分吸收塔顶气体。吸收后贫气里的C3含量由原来的7.5％，变成0.46％。吸收塔顶的干气经过节流与原料气换热后（温度34.28℃，压力0.39MPa）外输。吸收了多数丙烷的冷油（温度-13.54℃，压力1.28MPa）经过冷油泵增压到1.9MPa，输送至脱乙烷塔顶。
在浅冷轻烃回收工艺中，最主要的流程是对原料气进行丙烷或者氨冷却。具体流程为：丙烷气体进入压缩机压缩后，经过冷却器吸取压缩过程中产生的热量，丙烷液化到该压力下的露点，液化丙烷进入热虹吸丙烷储罐，储罐内液体丙烷进入经济器，以提高丙烷气化吸热的效率。经济器出来的丙烷经过节流阀，节流降温后进入丙烷储罐。液体丙烷进入原料气换热器，带走原料气的热量，从而达到降温的目的。经过换热气化后的丙烷蒸气通过丙烷液储罐进入压缩机，并开始下一个循环。
可以看出：丙烷制冷的工作原理包含丙烷压缩机、冷凝器、节流阀和蒸发器四个热力设备。包含压缩、冷凝、节流和吸热蒸发四个主要热力过程。采用该流程不但使得丙烷制冷循环需要设备多，投资大，能耗高；而且占用厂区内一定的空间。因此，从节能降耗方面来讲，采取新型轻烃浅冷回收工艺可使伴生气获得低温，并且获得最低的能耗。
发明内容
本发明的目的是提供一种浅冷轻烃回收工艺方法，采用四股流板翅式换热器和节流阀，通过装置中自产液烃不断冷却和节流，从而获得低温，将伴生气冷却至-25℃的低温，该工艺方法不仅节省了工厂的投资，而且节省了能源；经济效益和社会效益显著。
本发明所述的一种浅冷轻烃回收工艺方法，
原料气，温度25℃，压力0.3MPa，经过第一分离器分离后，原料气进入第一压缩机进行压缩，压缩后原料气进入第一冷却器，原料气经冷却至温度40℃，压力0.98MPa后，通过第一混合器进入第二分离器分离，分离后原料气进入第二压缩机进行增压，增压后原料气进入第二冷却器冷却至温度40℃，压力2.09MPa后进入第三分离器，分离出气体和液烃；温度40℃，压力2.09MPa的气体进入四股流板翅式换热器第一管程；经过冷却后，气体温度-22℃，压力2.07MPa，进入低温分离器；低温分离器出口气相经过第一节流阀节流后，温度-39.69℃，压力0.4MPa，进入四股板翅式流换热器第二管程提供冷量，换热后干气外输；出口干气温度25℃，压力0.38MPa，外输至下游，外输干气中的甲烷和乙烷含量为88.5％；
从低温分离器出来的液烃，经过分配器分成二股，一股通过第二节流阀，温度-32.34℃，压力1.0MPa的液烃进入四股流板翅式换热器第三管程给原料气提供冷量，换热后，温度35℃，压力0.98MPa的液烃进入第一混合器；第二股液烃经第三节流阀节流后，温度-24.72℃，压力1.7MPa进入到四股流板翅式换热器第四管程，给原料气提供冷量；换热后液烃温度35.88℃，压力1.68MPa，进入第三混合器；第一分离器、第二分离器通过第一液烃泵、第二液烃泵进入第三混合器，第三分离器液烃进入第三混合器；第三混合器的混合液烃进入脱乙烷塔，脱乙烷塔塔顶气体通过第四节流阀进入第一混合器；脱乙烷塔塔底混烃进入液化气塔；液化气塔塔顶气经第三冷却器外输液化气；液化气塔塔底轻油经第四冷却器外输轻油。
与压缩机二级出口分离器分离的液烃（温度40℃，压力2.09MPa）混合后进入脱乙烷塔。
该工艺通过自产液烃节流制冷对原料气进行反复冷却，最终制冷温度最低可达到-25℃。该工艺方法没有用传统的丙烷制冷或氨制冷方法，不仅节省占地面积，设备投资，更重要的是很大程度节省了能耗，通过能耗对比分析，节约的能耗比常规的浅冷冷凝+冷油吸收法省调了63.3％的能耗。
附图说明：
图1浅冷轻烃回收工艺流程图
其中，1、原料气；2、第一分离器；3、第一压缩机；4、第一冷却器；5、第一混合器；6、第二分离器；7、第二压缩机；8、第二冷却器；9、第三分离器；10、四股流板翅式换热器；11、低温分离器；12、第一节流阀；13、第二节流阀；14、第三节流阀；15、分配器；16、第三混合器；17、第四节流阀；18、脱乙烷塔；19、混烃；20、液化气塔；21第三冷却器；22、第四冷却器；23、外输轻油；24、外输液化气；25、第一液烃泵；26、第二液烃泵；27、外输干气
具体实施方式
表1是长庆油田姬一联合站伴生气组分表
表1伴生气组分表
（表中数据为长庆油田姬一联组分表，温度25℃，压力0.3MPa，流量55.69Kmol/h）
如图1所示，原料气1（温度25℃，压力0.3MPa）经过第一分离器2分离后，原料气进入第一压缩机3进行压缩，压缩后原料气进入第一冷却器4，原料气经冷却至温度40℃，压力0.98MPa后，通过第一混合器5进入第二分离器6分离，分离后原料气进入第二压缩机7进行增压，增压后原料气进入第二冷却器8冷却至温度40℃，压力2.09MPa后，进入第三分离器9，分离出气体和液烃；温度40℃，压力2.09MPa的气体进入四股流板翅式换热器10第一管程；经过冷却后，气体温度-22℃，压力2.07MPa，进入低温分离器11；低温分离器11出口气相经过第一节流阀12节流后，温度-39.69℃，压力0.4MPa，进入四股板翅式流换热器第二管程提供冷量，换热后干气27外输；出口干气温度25℃，压力0.38MPa，外输至下游，外输干气中的甲烷和乙烷含量为88.5％；
从低温分离器11出来的液烃，经过分配器15分成二股，一股通过第二节流阀13，温度-32.34℃，压力1.0MPa的液烃进入过四股流板翅式换热器10第三管程给原料气提供冷量，换热后，温度35℃，压力0.98MPa的液烃进入第一混合器5；第二股液烃经第三节流阀节流后，温度-24.72℃，压力1.7MPa进入到四股流板翅式换热器第四管程，给原料气提供冷量；换热后液烃温度35.88℃，压力1.68MPa，进入第三混合器16；第一分离器2、第二分离器6通过第一液烃泵、第二液烃泵进入第三混合器16，第三分离器9液烃进入第三混合器16；第三混合器16的混合液烃进入脱乙烷塔18，脱乙烷塔塔气体通过第四节流阀17进入第一混合器5；脱乙烷塔塔底混烃19进入液化气塔20；液化气塔塔顶气经第三冷却器21外输液化气24；液化气塔塔底轻油经第四冷却器22外输轻油。
与压缩机二级出口分离器分离的液烃（温度40℃，压力2.09MPa）混合后进入脱乙烷塔。
所述的脱乙烷塔塔顶压力设置在1.35MPa，塔底压力设置在1.4MPa。设置塔底加热温度在60℃.经过塔内蒸馏后，塔底液化气温度为37.8℃时的饱和蒸汽压为0.94MPa。
所述的塔底液化气含量（C3，iC4,nC4）为79.7％，达到了液化气外输的标准。
所述的塔顶贫气（温度33.09℃，压力1.35MPa）由于富含大量丙烷，约为45％，打循环回到二级压缩机入口再进行压缩、冷凝。
表2传统浅冷轻烃回收与新型浅冷回收工艺能耗对比表
能耗(kW) 传统浅冷轻烃回收工艺 新型浅冷轻烃回收工艺
一级压缩机和冷却器 82.27 136.55
二级压缩机和冷却器 157.55 288.1
丙烷系统 225.75 ——
脱乙烷塔底热负荷 124.9 43.79
液化气塔底热负荷 187.5 135.2
液烃增压泵 —— 0.146
从表中可以看出：
传统浅冷轻烃回收工艺能耗总计：777.97kW
新型浅冷轻烃回收工艺能耗总计：603.79kW
节能统计：(777.97-603.79)/777.97=22.4%。

Claims (1)

1.一种浅冷轻烃回收工艺方法，其特征在于：
第一原料气，温度25℃，压力0.3MPa，经过第一分离器分离后得到第二原料气，所述第二原料气进入第一压缩机进行压缩，压缩后的为第三原料气，所述第三原料气进入第一冷却器，所述第三原料气经冷却至温度40℃，压力0.98MPa后得到第四原料气，所述第四原料气通过第一混合器进入第二分离器分离，分离后得到第五原料气，所述第五原料气进入第二压缩机进行增压，增压后为第六原料气，所述第六原料气进入第二冷却器冷却至温度40℃，压力2.09MPa后得到第七原料气，所述第七原料气进入第三分离器，分离出第一气体和第三分离器液烃；温度40℃，压力2.09MPa的第一气体进入四股流板翅式换热器第一管程；经过冷却后得到第二气体，所述第二气体的温度-22℃，压力2.07MPa，进入低温分离器得到第三气体；所述第三气体经过第一节流阀节流后，温度-39.69℃，压力0.4MPa，进入四股流板翅式换热器第二管程提供冷量，换热后干气外输；出口干气温度25℃，压力0.38MPa，外输至下游；
从低温分离器出来得到第一液烃，所述第一液烃经过分配器分成二股，一股通过第二节流阀，温度-32.34℃，压力1.0MPa的液烃进入四股流板翅式换热器第三管程给所述第一气体提供冷量，换热后，温度35℃，压力0.98MPa的液烃进入第一混合器；第二股液烃经第三节流阀节流后，温度-24.72℃，压力1.7MPa进入到四股流板翅式换热器第四管程，给所述第一气体提供冷量，换热后液烃温度35.88℃，压力1.68MPa，进入第三混合器；第一分离器液烃、第二分离器液烃分别通过第一液烃泵、第二液烃泵进入第三混合器，第三分离器液烃进入第三混合器；第三混合器的混合液烃进入脱乙烷塔，脱乙烷塔塔顶气体通过第四节流阀进入第一混合器；脱乙烷塔塔底混烃进入液化气塔；液化气塔塔顶气经第三冷却器外输液化气；液化气塔塔底轻油经第四冷却器外输轻油。
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