CN111578619A - 一种回收烯烃火炬管网中轻烃和氮气的装置 - Google Patents

一种回收烯烃火炬管网中轻烃和氮气的装置 Download PDF

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CN111578619A
CN111578619A CN202010441818.2A CN202010441818A CN111578619A CN 111578619 A CN111578619 A CN 111578619A CN 202010441818 A CN202010441818 A CN 202010441818A CN 111578619 A CN111578619 A CN 111578619A
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nitrogen
light hydrocarbon
pipe network
olefin
tower
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孙郁
赵杰
杨晓京
程进杰
史红兵
张武
郝凯钟
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Zhongke Ruiao Energy Technology Co ltd
Technical Institute of Physics and Chemistry of CAS
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Technical Institute of Physics and Chemistry of CAS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/02—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
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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
    • F25J3/02—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
    • F25J3/0228—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
    • F25J3/0257—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 nitrogen
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    • F25J2210/12—Refinery or petrochemical off-gas
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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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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Abstract

本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，烯烃火炬管网中气体经过冷凝降温进入轻烃塔进行分离，轻烃塔的塔底精馏出轻烃产品，轻烃产品经过低温泵增压再经换热器降温后输送至烯烃分离装置进行分离，轻烃塔的顶部产品进入氮气塔，在氮气塔的塔顶产生氮气产品经换热器降温后再输送至氮气管网，而氮气塔的塔底产生的富甲烷气，经换热器降温后作为燃料气送入外部燃料气管网，本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，通过低温精馏分离的方式从火炬气管网中回收轻烃和氮气产品，回收过的轻烃产品作为烯烃原料直接送至烯烃分离装置进行分离，氮气产品作为补充氮气直接送入全厂氮气管网，使得火炬气中的有效组分充分利用，回收效益显著。

Description

一种回收烯烃火炬管网中轻烃和氮气的装置
技术领域
本发明涉及化工尾气的综合利用技术领域，特别涉及一种回收烯烃火炬管网中轻烃和氮气的装置。
背景技术
轻烃是重要的化工原料，在烯烃工厂中仍然有定期排放的排放点，且全厂阀门泄漏点较多，火炬气中始终存在大量的有效组分的直接排放，为了减少火炬气中有效组织的排放，部分工厂对火炬气用压缩机进行增压，水冷至40℃进行分离，回收其中的重组分后，轻组分直接排入燃料气管网进行燃烧，造成了资源的极大浪费。
在烯烃工厂，火炬气管网中有大量的有效组分，有较多较为昂贵的如：1,3丁二烯，反-2-丁烯、1-丁烯、异丁烯、顺-2-丁烯等。一个100万吨/年的烯烃工厂，火炬气的排放量约为1.5吨～3吨每小时，而其中有效组分的重量约在0.5吨～1吨每小时，按照轻烃每吨3000元计算，每小时燃烧掉1500元～3000元，按照每年8000小时计算，每年燃烧掉的费用约为1200万元～2400万元，而通过本装置进行回收，每年可获益1000万元～2000万元。
发明内容
有鉴如此，有必要针对现有技术存在的缺陷，提供一种可有效回收火炬气管网中轻烃和氮气的装置。
为实现上述目的，本发明采用下述技术方案：
一种回收烯烃火炬管网中轻烃和氮气的装置，包括：换热器、制冷压缩机、节流阀、低温泵、轻烃塔及氮气塔，其中：
外部制冷剂经所述压缩机压缩压缩后，再经循环水进行冷却进入所述换热器进行降温，并经过所述节流阀减压降温为所述换热器提供冷量；
烯烃火炬管网中气体经过换热器冷凝降温，进入所述轻烃塔进行分离，其中，所述轻烃塔的塔底精馏出轻烃产品，所述轻烃产品经过所述低温泵增压，再经所述换热器降温后输送至上游烯烃分离装置进行分离，所述轻烃塔的顶部产品进入所述氮气塔，在所述氮气塔的塔顶产生氮气产品，所述氮气产品经所述换热器降温后再输送至氮气管网，而所述氮气塔的塔底产生的富甲烷气，经所述换热器降温后作为燃料气送入外部燃料气管网。
在一些较佳的实施例中，所述烯烃火炬管网中气体包含氮气、氢气、甲烷、乙烷、乙烯、丙烷、丙烯、正丁烷、异丁烷、反-2-丁烯、1-丁烯、异丁烯、顺-2-丁烯、1,3丁二烯、戊烷或异戊烷。
在一些较佳的实施例中，所述换热器为板翅式换热器或绕管式换热器。
在一些较佳的实施例中，所述制冷压缩机为离心式压缩机、往复式压缩机或螺杆式压缩机。
在一些较佳的实施例中，所述轻烃塔及氮气塔为板式塔或填料塔或泡罩塔或浮阀塔。
在一些较佳的实施例中，所述氮气产品中N2含量＞99％。
在一些较佳的实施例中，所述制冷压缩机的制冷循环为混合冷剂制冷循环、氮气膨胀制冷循环或尾气膨胀制冷循环。
本发明采用上述技术方案的优点是：
本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，烯烃火炬管网中气体经过冷凝降温，进入所述轻烃塔进行分离，其中，所述轻烃塔的塔底精馏出轻烃产品，所述轻烃产品经过所述低温泵增压，再经所述换热器降温后输送至上游烯烃分离装置进行分离，所述轻烃塔的顶部产品进入所述氮气塔，在所述氮气塔的塔顶产生氮气产品，所述氮气产品经所述换热器降温后再输送至氮气管网，而所述氮气塔的塔底产生的富甲烷气，经所述换热器降温后作为燃料气送入外部燃料气管网，本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，通过低温精馏分离的方式从火炬气管网中回收轻烃和氮气产品，回收过的轻烃产品作为烯烃原料直接送至烯烃分离装置进行分离，氮气产品作为补充氮气直接送入全厂氮气管网，使得火炬气中的有效组分充分利用，循环利用，变废为宝，回收效益显著，该装置稳定可靠，能耗低。
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它的附图。
图1为本发明实施例提供的回收烯烃火炬管网中轻烃和氮气的装置的结构示意图。
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做出创造性劳动前提下所获得的所有其它实施例，都属于本发明保护的范围。
请参阅图1，为本发明实施例提供的回收烯烃火炬管网中轻烃和氮气的装置的结构示意图，包括：换热器110、制冷压缩机120、节流阀130、低温泵140、轻烃塔150及氮气塔160。
本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，冷量均有制冷压缩机120和换热器110提供，外部制冷剂首先经制冷压缩机120压缩至15bar(A)～21bar(A)，然后经循环水进行冷却，冷却至40℃，进入换热器110进行降温至-160℃，然后经过节流阀130，减压降温，为换热器110提供冷量。
在一些较佳实施例中，所述换热器110为板翅式换热器或绕管式换热器。
在一些较佳实施例中，所述制冷压缩机120为离心式压缩机、往复式压缩机或螺杆式压缩机。
进一步地，所述制冷压缩机120的制冷循环为混合冷剂制冷循环、氮气膨胀制冷循环或尾气膨胀制冷循环。
在一些较佳实施例中，所述轻烃塔150及氮气塔160为板式塔或填料塔或泡罩塔或浮阀塔，其中：板式塔塔板数量可以从0～50块，填料塔填料高度可以从0～30米。
本发明提供的回收烯烃火炬管网中轻烃和氮气的装置的工作方式如下：
火炬管网气体经过换热器110降温至-140～-160℃后，进入轻烃塔150进行气液分离，其中，所述轻烃塔150的塔底精馏出轻烃产品经过低温泵140增压至6barG～50barG后进入换热器110复温后作为轻烃产品输送至上游烯烃分离装置进行分离；所述轻烃塔150的顶部产品进入所述氮气塔160，所述氮气塔160对所述轻烃塔150的气相组分进一步精馏分离，在所述氮气塔160的塔顶产生氮气产品，所述氮气产品经所述换热器110降温后再输送至氮气管网，而所述氮气塔160的塔底产生的富甲烷气，经所述换热器110降温后作为燃料气送入外部燃料气管网。
在一些较佳的实施例中，所述烯烃火炬管网中气体包含氮气、氢气、甲烷、乙烷、乙烯、丙烷、丙烯、正丁烷、异丁烷、反-2-丁烯、1-丁烯、异丁烯、顺-2-丁烯、1,3丁二烯、戊烷或异戊烷。
本发明提供的回收烯烃火炬管网中轻烃和氮气的装置，通过低温精馏分离的方式从火炬气管网中回收轻烃和氮气产品，回收过的轻烃产品作为烯烃原料直接送至烯烃分离装置进行分离，氮气产品作为补充氮气直接送入全厂氮气管网，使得火炬气中的有效组分充分利用，循环利用，变废为宝，回收效益显著，该装置稳定可靠，能耗低。
以上所述实施例的各技术特征可以进行任意的组合，为使描述简洁，未对上述实施例中的各个技术特征所有可能的组合都进行描述，然而，只要这些技术特征的组合不存在矛盾，都应当认为是本说明书记载的范围。
当然本发明的回收烯烃火炬管网中轻烃和氮气的装置正极材料还可具有多种变换及改型，并不局限于上述实施方式的具体结构。总之，本发明的保护范围应包括那些对于本领域普通技术人员来说显而易见的变换或替代以及改型。

Claims (7)

1.一种回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，包括：换热器、制冷压缩机、节流阀、低温泵、轻烃塔及氮气塔，其中：
外部制冷剂经所述压缩机压缩压缩后，再经循环水进行冷却进入所述换热器进行降温，并经过所述节流阀减压降温为所述换热器提供冷量；
烯烃火炬管网中气体经过所述换热器冷凝降温，进入所述轻烃塔进行分离，其中，所述轻烃塔的塔底精馏出轻烃产品，所述轻烃产品经过所述低温泵增压，再经所述换热器降温后输送至上游烯烃分离装置进行分离，所述轻烃塔的顶部产品进入所述氮气塔，在所述氮气塔的塔顶产生氮气产品，所述氮气产品经所述换热器降温后再输送至氮气管网，而所述氮气塔的塔底产生的富甲烷气，经所述换热器降温后作为燃料气送入外部燃料气管网。
2.根据权利要求1所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述烯烃火炬管网中气体包含氮气、氢气、甲烷、乙烷、乙烯、丙烷、丙烯、正丁烷、异丁烷、反-2-丁烯、1-丁烯、异丁烯、顺-2-丁烯、1,3丁二烯、戊烷或异戊烷。
3.根据权利要求1所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述换热器为板翅式换热器或绕管式换热器。
4.如权利要求1所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述制冷压缩机为离心式压缩机、往复式压缩机或螺杆式压缩机。
5.如权利要求1所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述轻烃塔及氮气塔为板式塔或填料塔或泡罩塔或浮阀塔。
6.如权利要求1所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述氮气产品中N2含量＞99％。
7.如权利要求4所述的回收烯烃火炬管网中轻烃和氮气的装置，其特征在于，所述制冷压缩机的制冷循环为混合冷剂制冷循环、氮气膨胀制冷循环或尾气膨胀制冷循环。
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