CN105461504B - 一种组合吸收塔、尾气膨胀系统及尾气回收方法 - Google Patents

一种组合吸收塔、尾气膨胀系统及尾气回收方法 Download PDF

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CN105461504B
CN105461504B CN201410462689.XA CN201410462689A CN105461504B CN 105461504 B CN105461504 B CN 105461504B CN 201410462689 A CN201410462689 A CN 201410462689A CN 105461504 B CN105461504 B CN 105461504B
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CN105461504A (zh
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刘洪谦
王子宗
李广华
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Sinopec Engineering Inc
Sinopec Engineering Group Co Ltd
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Abstract

本发明公开了一种组合吸收塔、尾气膨胀系统及尾气回收方法。所述组合吸收塔下部为吸收塔段，塔上部为深冷精馏塔段；吸收塔段和深冷精馏段通过管线连接；所述深冷精馏塔段是一个内部填满精馏填料的板翅式分凝分馏器。所述尾气膨胀系统包括:组合吸收塔、膨胀机、气液分离罐和冷箱；组合吸收塔的深冷精馏塔段顶部依次连接膨胀机和气液分离罐，气液分离罐的顶部和底部出口分别连接组合吸收塔的深冷精馏塔段后，连接冷箱。本发明可以提高轻烃回收装置的收率、减小吸收剂损失，进一步降低轻烃回收部分的投资和能耗。

Description

一种组合吸收塔、尾气膨胀系统及尾气回收方法
技术领域
本发明涉及轻烃尾气回收领域，进一步地说，是涉及一种组合吸收塔、尾气膨胀系统及尾气回收方法。
背景技术
CN202081036U发明的甲醇制丙烯(MTP)产品气轻烃回收方法，采用的是在脱甲烷塔塔顶安放尾气过冷器来减小乙烯损失，过冷器的冷量来自脱甲烷塔尾气膨胀制冷或节流制冷。
CN101747128B在脱甲烷塔顶设置膨胀机，在脱甲烷塔内设置内置式冷凝器，将作为吸收剂的-40℃的丙烷或混合C3加到脱甲烷塔顶部的塔板上。脱甲烷塔内的气相物流，经过内置式冷凝器冷却到－45℃～－60℃，从脱甲烷塔塔顶出来的气相进入膨胀机，将温度过冷到－90℃～－120℃，压力降到0.1MPaG～0.6MPaG，出膨胀机的物流进行气液分离，其中气体物流复热后出界区，液相物流进气体压缩机前二段吸入罐，或返回脱甲烷塔，脱甲烷塔底物流进入其他烯烃分离单元分离出乙烯和丙烯产品，所述脱甲烷塔吸收剂为C3、C4和C5+馏分中的一种以上物质。该专利实际应用时经常遇到尾气中乙烯含量超标现象。
US20140135558A1为回收脱甲烷塔尾气中的乙烯，在脱甲烷塔顶部安放一个吸收塔段，脱甲烷塔和吸收塔冷凝器均使用-40℃的丙烯冷剂做冷媒。吸收塔用C2～C10烃类或其混合物做吸收剂，该专利使用丙烷或混合C3做吸收剂。
为提高尾气中乙烯的收率、回收夹带的吸收剂(C3)，该专利将低温乙烷同低温甲烷尾气混合后为吸收塔尾气进行激冷，再次回收乙烯和夹带的吸收剂。
许多专利都集中在如何回收脱甲烷塔尾气中的乙烯，但这些专利无法回避不凝气夹带吸收剂的问题。
发明内容
为解决现有技术中出现的问题，本发明提供了一种组合吸收塔、尾气膨胀系统及尾气回收方法。本发明的组合吸收塔用于轻烃尾气回收或从脱甲烷塔尾气中回收乙烯等物质。本发明使得脱轻烃尾气如甲烷塔尾气先经过中冷油吸收回收其中的乙烯，未吸收完的尾气直接经过深冷精馏塔段回收其中剩余的乙烯和被夹带的吸收剂。本发明可以提高轻烃回收装置的收率、减小吸收剂损失，进一步降低轻烃回收部分的投资和能耗。
本发明的目的之一是提供一种组合吸收塔。
所述组合吸收塔下部为吸收塔段，塔上部为深冷精馏塔段；吸收塔段和深冷精馏段通过管线连接；
所述深冷精馏塔段是一个内部填满精馏填料的板翅式分凝分馏器。
所述吸收塔段为板式塔形式或填料塔形式。
本发明的目的之二是提供一种尾气膨胀系统。
包括:组合吸收塔、膨胀机、气液分离罐和冷箱；
组合吸收塔的深冷精馏塔段顶部依次连接膨胀机和气液分离罐，气液分离罐的顶部和底部出口分别连接组合吸收塔的深冷精馏塔段后，连接冷箱。
本发明的目的之三是提供一种尾气回收方法。
包括:
1)尾气从组合吸收塔底部进入吸收塔段，吸收剂从吸收塔段顶部进入，吸收完的吸收剂富液从吸收塔段底部离开组合吸收塔；
2)未吸收完的气体从吸收塔段顶部向上进入深冷精馏塔段底部，然后以不凝气形式从深冷精馏塔段顶部离开组合吸收塔；深冷精馏塔段底部液相物料作为吸收塔段吸收剂的一部分，依靠重力自流回吸收塔段顶部；
3)自组合吸收塔深冷精馏塔段顶部出来的不凝气，经膨胀制冷后进气液分离罐进行气液分离，分离出来的气液相分别经过深冷精馏塔段和冷箱复热，复热后的气相升压后去燃料气系统，复热后的液相去返回装置前端。
4)深冷精馏塔段的冷量由冷媒和膨胀制冷后的深冷精馏塔段顶部不凝气联合提供。
其中，优选：
所述深冷精馏塔段的温度为-85℃～-108℃；
所述尾气为-30℃～-40℃、2.5MPaG～3.0MPaG的脱甲烷塔尾气。
本发明具体技术方案如下：
本发明所述组合吸收塔：
(1)组合吸收塔上部是优选工作温度为-85℃～-108℃的深冷精馏塔段，下部是吸收塔段。
(2)深冷精馏塔段是一个内部充满精馏填料的板翅式分凝分馏器。
(3)被吸收的轻烃尾气如脱甲烷塔塔顶尾气从底部进入组合吸收塔的吸收塔段，气体在吸收塔段内继续上行至组合吸收塔上部的深冷精馏塔段,深冷精馏塔段底部液相物料作为吸收塔段吸收剂的一部分，依靠重力自流回吸收塔段顶部，深冷精馏塔段不凝气离开组合吸收塔去膨胀制冷。
(4)自组合吸收塔深冷精馏塔段顶部出来的不凝气，优选操作温度和压力分别为－85℃～－108℃、2.5～3.0MPaG，该不凝气经膨胀制冷后进气液分离罐进行气液分离，分离出来的气液相分别经过深冷精馏塔段复热，复热后的气相升压后去燃料气系统，复热后的液相去返回装置前端。
(5)深冷精馏塔段的冷量由-40℃丙烯冷剂和膨胀制冷后的深冷精馏塔段不凝气联合提供。
本发明的组合吸收塔适用于所有富产低碳轻烃工业装置，如甲醇制烯烃(MTO)装置、甲醇制芳烃(MTA)装置，优选应用于MTP装置。
本发明和现有技术相比：
采用组合吸收塔能有效地降低尾气中乙烯和吸收剂的损失。
本发明主要针对从产品气丙烯乙烯质量比(P/E)>>1的轻烃装置尾气回收，尤其针对甲醇制丙烯(MTP)装置脱甲烷塔尾气回收，也同样适用于其他富产高丙烯含量低碳烯烃气体的工业装置的尾气回收，如催化裂解制烯烃CPP、深度催化裂解DCC、烯烃催化裂解OCC、Superflex、ACO等。
附图说明
图1本发明的组合吸收塔示意图；
图2组合吸收塔尾气膨胀回收系统示意图。
附图标记说明：
设备标记说明：
1-组合吸收塔，2-吸收塔段，3-深冷精馏塔段，4-膨胀机，5-气液分离罐，6-冷箱。
物流标记说明：
100-脱甲烷塔塔顶尾气，101-不凝气，102-膨胀机出口物流，103-气液分离罐底部液体，104-气液分离罐顶部的不凝气，105-丙烯冷剂，106-复热后液体，107-复热后气体，108-吸收剂富液，110-吸收剂。
具体实施方式
下面结合实施例，进一步说明本发明。
实施例：
如图1所示，一种组合吸收塔1。所述组合吸收塔1下部为吸收塔段2，塔上部为深冷精馏塔段3；吸收塔段2和深冷精馏塔段3通过管线连接；
所述深冷精馏塔段3是一个内部填满精馏填料的板翅式分凝分馏器。
所述吸收塔段2采用填料塔形式。
如图2所示，一种尾气膨胀系统。
包括：组合吸收塔1、膨胀机4、气液分离罐5和冷箱6；
组合吸收塔1的深冷精馏塔段3顶部依次连接膨胀机4和气液分离罐5，气液分离罐5的顶部和底部出口分别连接组合吸收塔1的深冷精馏塔段3后，连接冷箱6。
针对甲醇制丙烯(MTP)脱甲烷塔尾气回收：
组合吸收塔1吸收塔段2顶部出口直接连着深冷精馏塔段3和冷箱6，被吸收的脱甲烷塔尾气气体100从底部进入吸收塔段2，再从吸收塔段2的顶部进入深冷精馏塔段3,深冷精馏塔段3工艺侧的凝液依靠重力返回吸收塔段2的顶部，深冷精馏塔段3顶部的不凝气经膨胀机4膨胀制冷后进入气液分离罐5。
气液分离罐5顶部不凝气104节流后经深冷精馏塔段3和冷箱6复热后经过再压缩机升压去燃料气系统，气液分离罐5底部液体经深冷精馏塔段3复热后返回产品气压缩系统。
吸收剂110进入组合吸收塔吸收塔段2的顶部，并从吸收塔段2底部以富液108形式离开组合吸收塔1。
深冷精馏塔段的冷量由-40℃丙烯冷剂105和膨胀制冷后的深冷精馏塔段不凝气102联合提供。
深冷精馏塔段顶部温度为－99℃、操作压力为2.5PaG。
MTP脱甲烷塔尾气100、复热后的气液分离罐5顶部和底部气液相组成如表1所示。
表1 MTP脱甲烷塔尾气回收关键物流参数
采用通用的Simsci公司的Provision 7.0流程模拟软件，对本实施例的流程方案进行模拟。
对比例
以实施例脱甲烷塔尾气组成为基础，采用专利CN101747128B的技术方案回收深冷精馏塔段3不凝气中的乙烯。乙烯和吸收剂的损失，见表2。
表2
从表2可以看到，专利CN101747128B不凝气107中乙烯损失为112.0 T/A，吸收剂(C4s、C5s和C6+总和)损失为7.0T/A，本发明实例不凝气107中的乙烯和吸附剂损失最小，可以忽略不计。
从设备上看，CN101747128B脱甲烷塔内置冷凝器是一个板翅式换热器，本发明的深冷精馏塔段也是由板翅式换热器演变而来，但在物流侧充满了精馏填料，两者设备投资相差不大，而分离消耗和冷能利用率却天壤之别。

Claims (8)

1.一种组合吸收塔，其特征在于：
所述组合吸收塔下部为吸收塔段，塔上部为深冷精馏塔段；吸收塔段和深冷精馏段通过管线连接；
所述深冷精馏塔段是一个内部填满精馏填料的板翅式分凝分馏器。
2.如权利要求1所述的组合吸收塔，其特征在于:
所述吸收塔段为板式塔形式或填料塔形式。
3.一种采用如权利要求1或2所述的组合吸收塔的尾气膨胀装置，其特征在于：
所述尾气膨胀装置包括:组合吸收塔、膨胀机、气液分离罐和冷箱；
组合吸收塔的深冷精馏塔段顶部依次连接膨胀机和气液分离罐，气液分离罐的顶部和底部出口分别连接组合吸收塔的深冷精馏塔段后，连接冷箱。
4.一种采用如权利要求1或2所述的组合吸收塔的尾气回收方法，其特征在于所述方法包括:
1)尾气从组合吸收塔底部进入吸收塔段，吸收剂从吸收塔段顶部进入，吸收完的吸收剂富液从吸收塔段底部离开组合吸收塔；
2)未吸收完的气体从吸收塔段顶部向上进入深冷精馏塔段底部，然后以不凝气形式从深冷精馏塔段顶部离开组合吸收塔；深冷精馏塔段底部液相物料作为吸收塔段吸收剂的一部分，依靠重力自流回吸收塔段顶部。
5.如权利要求4所述的尾气回收方法，其特征在于所述方法包括:
3)自组合吸收塔深冷精馏塔段顶部出来的不凝气，经膨胀制冷后进气液分离罐进行气液分离，分离出来的气液相分别经过深冷精馏塔段和冷箱复热，复热后的气相升压后去燃料气系统，复热后的液相去返回装置前端。
6.如权利要求5所述的尾气回收方法，其特征在于：
4)深冷精馏塔段的冷量由冷媒和膨胀制冷后的深冷精馏塔段顶部不凝气联合提供。
7.如权利要求4所述的尾气回收方法，其特征在于：
所述深冷精馏塔段的温度为‐85℃～‐108℃。
8.如权利要求7所述的尾气回收方法，其特征在于：
所述尾气为‐30℃～‐40℃、2.5MPaG～3.0MPaG的脱甲烷塔尾气。
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