CN114616042A - 用于从丙烷脱氢工艺回收丙烯的方法 - Google Patents

用于从丙烷脱氢工艺回收丙烯的方法 Download PDF

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CN114616042A
CN114616042A CN202080075419.7A CN202080075419A CN114616042A CN 114616042 A CN114616042 A CN 114616042A CN 202080075419 A CN202080075419 A CN 202080075419A CN 114616042 A CN114616042 A CN 114616042A
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R·列伊涅克
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Kellogg Brown and Root LLC
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Abstract

在丙烷脱氢(PDH)工艺中，脱乙烷塔和冷却列系统的目的是将裂解的气体分离成富甲烷尾气产品、C2工艺流和C3工艺流。本文所述的方法通过使用分阶段冷却、对进料至反应器的丙烷进料的工艺至工艺的互换和使用高效热交换器和分布式蒸馏技术，降低了制冷功率要求，并提供了简单且可靠的设计。

Description

用于从丙烷脱氢工艺回收丙烯的方法
技术领域
本发明涉及一种用于从丙烷脱氢(PDH)工艺回收丙烯的方法，更具体地，涉及从PDH工艺回收富甲烷、富C2和富C3的产品。
背景
丙烷脱氢(PDH)是由丙烷制备丙烯的工艺步骤。PDH对石油化工行业很重要，因为丙烯是石油化工行业中次于乙烯的第二重要的起始产品。在PDH工艺中，脱乙烷塔和冷却列系统的目的是将裂解的气体分离成富甲烷尾气产品、C2工艺物流和C3工艺物流。改进PDH工艺，例如通过减少制冷功率要求、简化设计和/或使设计更可靠，总是有益的。
附图简述
图1是如本文所述的PDH工艺的非限制性示意图。
概述
在一个非限制性实施方案中，提供了一种用于从包括丙烷脱氢(PDH)反应器的PDH工艺回收丙烯的方法，其中所述方法包括：将来自工艺气体干燥器的干燥工艺气体进料至第一脱乙烷塔进料冷却器，并用丙烷将其冷却；将冷却的干燥工艺气体送至第一脱乙烷塔进料筒；将来自第一脱乙烷塔进料筒的液体进料至脱乙烷塔；将来自第一脱乙烷塔进料筒的顶部蒸气送至工艺气体压缩机(PGC)；在第二脱乙烷塔进料冷却器中用丙烷，然后在第三脱乙烷塔进料冷却器中用丙烯制冷剂，冷却来自PGC的排出物，并将排出物送至第二脱乙烷塔进料筒；将来自第二脱乙烷塔进料筒的液体进料至脱乙烷塔；在冷箱中冷却并部分地冷凝来自第二脱乙烷塔进料筒的蒸气；将来自冷箱的工艺流出物在第一冷筒中分离成气相和液相；在冷箱中将来自第一冷筒的液体蒸发，并将其循环至PGC的第一级；重新加热来自第一冷筒的蒸气至成为富甲烷尾气产品；在脱乙烷塔中将乙烷和较轻的组分与C3和较重的组分分离；在脱乙烷塔再沸器中用淬火水或丙烯制冷剂蒸气使脱乙烷塔底部液体再沸，并在脱乙烷塔冷凝器中用丙烯制冷剂部分地冷凝顶部蒸气；在脱乙烷塔回流筒中，将来自脱乙烷塔冷凝器的工艺流出物分离成气相和液相，并将气相送至冷箱，并将液体返回至脱乙烷塔；从脱乙烷塔的上部进料阶段上方提取液体物流，泵送该液体物流，然后任选地将其在第一泵循环冷却器中用丙烷、然后在第二泵循环冷却器中用丙烯制冷剂进行冷却，并将冷却的液体在高于提取塔盘的位置处返回至脱乙烷塔中；将脱乙烷塔底部液体进料至C3分离器；和冷箱使来自第一冷筒的尾气、PGC循环物流、富C2物流和进料至PDH反应器的丙烷进料过热，同时还使液体丙烯制冷剂过冷。
在一个非限制性形式中，另外提供了一种用于从包括丙烷脱氢(PDH)反应器的PDH工艺回收丙烯的系统，其中所述系统包括：工艺气体干燥器，其被配置为将干燥工艺气体进料至第一脱乙烷塔进料冷却器并用丙烷使其冷却；第一脱乙烷塔进料筒，其被配置为接收来自第一脱乙烷塔进料冷却器的干燥工艺气体；脱乙烷塔，其被配置为接收来自第一脱乙烷塔进料筒的液体；工艺气体压缩机(PGC)，其被配置为接收来自第一脱乙烷塔进料筒的顶部蒸气；第二脱乙烷塔进料冷却器，其被配置为用丙烷冷却来自PGC的排出物；第三脱乙烷塔进料冷却器，其被配置为用丙烯制冷剂冷却来自PGC的排出物；第二脱乙烷塔进料筒，其被配置为接收来自第三脱乙烷塔进料冷却器的排出物，并将进料液体送至脱乙烷塔；冷箱，其被配置为接收、冷却和部分地冷凝来自第二脱乙烷塔进料筒的蒸气；第一冷筒，其被配置为将来自冷箱的工艺流出物分离成气相和液相，并将蒸发的液体循环至PGC的第一级；顶部脱乙烷塔冷凝器，其被配置为用丙烯制冷剂部分地冷凝顶部蒸气；脱乙烷塔回流筒，其被配置为将来自顶部脱乙烷塔冷凝器的工艺流出物分离成蒸气和液体，将气相送至冷箱；管线，其将来自脱乙烷塔回流筒的液体导引至脱乙烷塔；和C3分离器，其被配置为接收来自脱乙烷塔的底部液体。任选地，所述系统可另外包括脱乙烷塔再沸器，其被配置为用丙烯制冷剂蒸气再沸脱乙烷塔底部液体。
详述
已经发现，通过使用分阶段冷却、对进料至反应器的丙烷进料的工艺至工艺的互换和使用高效热交换器和分布式蒸馏技术，降低了制冷功率要求，并为丙烷脱氢(PDH)工艺提供了简单且可靠的设计。
更详细地，并参考图1，当一起看时，其是如本文所述方法的完整但非限制性示意图，干燥工艺气体和液体被进料至脱乙烷塔系统。更具体地说，来自工艺气体干燥器(未显示--来自图1的左边)的干燥工艺气体1在第一脱乙烷塔进料冷却器20中被来自丙烷入口物流15的丙烷冷却，并作为气体2被送至第一脱乙烷塔进料筒22。来自第一脱乙烷塔进料筒22的液体4被进料至脱乙烷塔24，在一个非限制性形式中，通过用冷凝物泵52泵送进料至脱乙烷塔24。顶部蒸气到达第三级工艺气体压缩机(PGC)26。来自工艺气体压缩机26的排出物3在第二脱乙烷塔进料冷却器28中被同样来自丙烷入口物流15的丙烷冷却，然后在第三脱乙烷塔进料冷却器30中被丙烯制冷剂冷却，并送至第二脱乙烷塔进料筒2号(V-4002)。来自第二脱乙烷塔进料筒2号(V-4002)32的液体6被进料至脱乙烷塔24。来自第二脱乙烷塔进料冷却器28的丙烷14在被进料至PDH反应器之前被送到冷箱34。
来自第二脱乙烷塔进料筒32的蒸气5在冷箱34中被冷却并部分冷凝。来自冷箱34的工艺流出物在第一冷筒36中被分离成气相和液相。来自第一冷筒36的液体12在冷箱34中被蒸发，并循环至PGC第一级，以回收包含的丙烯。来自第一冷筒36的蒸气被重新加热，并成为富甲烷尾气产品13。
脱乙烷塔24将乙烷和较轻的组分与C3和较重的组分分离。脱乙烷塔底部液体在脱乙烷塔再沸器38中被淬火水或丙烯制冷剂蒸气再沸。顶部蒸气在脱乙烷塔冷凝器40中被丙烯制冷剂部分冷凝。脱乙烷塔冷凝器40的工艺流出物在脱乙烷塔回流筒42中被分离成气相和液相。气相7到达冷箱34。液体被导引回至脱乙烷塔24，任选地由脱乙烷塔回流泵44泵送。脱乙烷塔底部液体作为原料进至C3分离器。
脱乙烷塔24上段上的泵循环9在脱乙烷塔第一泵循环冷却器46中被来自丙烷进口物流15的丙烷冷却，并在脱乙烷塔第二泵循环冷却器48中被中级丙烯制冷剂冷却，并且冷却的物流10在较高的塔盘位置返回至脱乙烷塔24，以减少对顶部脱乙烷塔冷凝器40上的低级制冷剂的要求。
冷箱34过热来自第一冷筒36的尾气、PGC循环物流12、富C2物流11和至反应器的丙烷，同时过冷液体丙烯制冷剂16。
脱乙烷塔底部物流8进料至热泵式C3分离器，在那里聚合物级丙烯与丙烷循环和C4+组分分离。在一个非限制性实施方案中，大部分丙烷循环被作为侧馏分取自绕过脱丙烷塔的C3分离器，而剩余的C3循环和C4+物质被循环至脱丙烷塔(未显示)，在那里C4+与新鲜进料和循环丙烷分离。
在一个非限制性实施方案中，该方法的某些设备的操作条件范围可如表I中所给出。
表I
用于在PDH工艺中回收丙烯的操作条件
名称 温度 压力
第一脱乙烷塔进料筒22 10℃至-5℃ 10–15barg
第二脱乙烷塔进料筒32 -25℃至-40℃ 20–40barg
脱乙烷塔24 -40℃(顶部)至+40℃底部 10–15barg
脱乙烷塔回流筒42 -30℃至-40℃ 10–15barg
第一冷筒36 -40℃至-100℃ 20–40barg
冷箱34 -120℃至+40℃
本文所述的用于从PDH工艺回收丙烯的方法具有许多优点，包括但不限于降低的功率要求、高丙烯回收率、更简单的设计和增加的可靠性。在一个非限制性实施方案中，使用液态丙烷进料至反应器，以首先向该工艺提供制冷，导致与脱丙烷塔顶部作为蒸气产生并直接进料至反应器的设计相比约30％至50％范围的功率节省。为简单起见，该设计仅使用丙烯制冷系统，但通过循环第一冷筒1号中产生的液体并将其用作冷箱中的冷却介质，仍然实现了良好的丙烯回收。
在上述说明书中，已经参照其具体实施方案对本发明进行了描述。然而，本说明书应被视为说明性的而非限制性的意义。例如，落入要求保护的或公开的参数但未在具体实施例中具体确定或尝试的设备、工艺和操作条件，预期将在本发明的范围内。
本发明可在不存在未公开的元素的情况下实施。此外，本发明可适当地包括所公开的元素、由所公开的元素组成或基本由所公开的元素组成。例如，可提供一种用于从包括PDH反应器的PDH工艺回收丙烯的方法，其中该方法进一步基本由以下组成或由以下组成：
将来自工艺气体干燥器的干燥工艺气体进料至第一脱乙烷塔进料冷却器，并用丙烷将其冷却；
将冷却的干燥工艺气体送至第一脱乙烷塔进料筒；
将来自第一脱乙烷塔进料筒的液体进料至脱乙烷塔；
将来自第一脱乙烷塔进料筒的顶部蒸气送至工艺气体压缩机(PGC)；
在第二脱乙烷塔进料冷却器中用丙烷，然后在第三脱乙烷塔进料冷却器中用丙烯制冷剂，冷却来自PGC的排出物，并将该排出物送至第二脱乙烷塔进料筒；
将来自第二脱乙烷塔进料筒的液体进料至脱乙烷塔；
在冷箱中冷却并部分地冷凝来自第二脱乙烷塔进料筒的蒸气；
将来自冷箱的工艺流出物在第一冷筒中分离成气相和液相；
在冷箱中将来自第一冷筒的液体蒸发，并将其循环至PGC的第一级；
重新加热来自第一冷筒的蒸气至成为富甲烷尾气产品；
在脱乙烷塔中将乙烷和较轻的组分与C3和较重的组分分离；
在脱乙烷塔再沸器中用淬火水或丙烯制冷剂蒸气使脱乙烷塔底部液体再沸，并在脱乙烷塔冷凝器中用丙烯制冷剂部分地冷凝顶部蒸气；
在脱乙烷塔回流筒中，将来自脱乙烷塔冷凝器的工艺流出物分离成气相和液相，并将气相送至冷箱，并将液体返回至脱乙烷塔，任选地通过脱乙烷塔回流泵；
从脱乙烷塔的上部进料阶段上方提取液体物流，泵送该液体物流，然后将其在第一泵循环冷却器中用丙烷、然后在第二泵循环冷却器中用丙烯制冷剂进行冷却，并将冷却的液体在高于提取塔盘的位置处返回至脱乙烷塔中；
将脱乙烷塔底部液体进料至C3分离器；和
冷箱使来自第一冷筒的尾气、PGC循环物流、富C2物流和进料至PDH反应器的丙烷进料过热，同时还使液体丙烯制冷剂过冷。
供选择地，可提供一种用于从包括丙烷脱氢(PDH)反应器的PDH工艺回收丙烯的系统，其中该系统基本上由以下组成或由以下组成：
工艺气体干燥器，其被配置为将干燥工艺气体进料至第一脱乙烷塔进料冷却器并用丙烷使其冷却；
第一脱乙烷塔进料筒，其被配置为接收来自第一脱乙烷塔进料冷却器的干燥工艺气体；
脱乙烷塔，其被配置为接收来自第一脱乙烷塔进料筒的液体；
工艺气体压缩机(PGC)，其被配置为接收来自第一脱乙烷塔进料筒的顶部蒸气；
第二脱乙烷塔进料冷却器，其被配置为用丙烷冷却来自PGC的排出物；
第三脱乙烷塔进料冷却器，其被配置为用丙烯制冷剂冷却来自PGC的排出物；
第二脱乙烷塔进料筒，其被配置为接收来自第三脱乙烷塔进料冷却器的排出物，并将进料液体送至脱乙烷塔；
冷箱，其被配置为接收、冷却和部分地冷凝来自第二脱乙烷塔进料筒的蒸气；
第一冷筒，其被配置为将来自冷箱的工艺流出物分离成气相和液相，并将蒸发的液体循环至PGC的第一级；
顶部脱乙烷塔冷凝器，其被配置为用丙烯制冷剂部分地冷凝顶部蒸气；
脱乙烷塔回流筒，其被配置为将来自顶部脱乙烷塔冷凝器的工艺流出物分离成蒸气和液体，将气相送至冷箱；
管线，其将来自脱乙烷塔回流筒的液体导引至脱乙烷塔；和
C3分离器，其被配置为接收来自脱乙烷塔的底部液体。在另一个非限制性供选择的实施方案中，该系统还可基本包括或包括脱乙烷塔再沸器，其被配置为用丙烯制冷剂蒸气再沸脱乙烷塔底部液体。
如在整个权利要求书中使用的词语“包括(comprising)”和“包括(comprises)”应分别解释为是指“包括(including)但不限于”和“包括(includes)但不限于”。
如本文所使用的，词语“基本上”应指“大体上是但不完全是所指定的”。
如本文所使用的，单数形式“一(a)”、“一个(an)”和“所述”旨在也包括复数形式，除非上下文明确地以其它方式指出。
如本文所使用的，术语“约”在提及给定参数时包括所述值，并具有由上下文确定的含义(例如，其包括与给定参数的测量相关的误差程度)。
如本文所使用的，术语“和/或”包括一个或多个相关列出项目的任何和所有组合。

Claims (10)

1.一种从包括丙烷脱氢(PDH)反应器的PDH工艺中回收丙烯的方法，所述方法包括：
将来自工艺气体干燥器的干燥工艺气体(1)进料至第一脱乙烷塔进料冷却器(20)，并用丙烷将其冷却；
将冷却的干燥工艺气体(2)送至第一脱乙烷塔进料筒(22)；
将来自第一脱乙烷塔进料筒(22)的液体(4)进料至脱乙烷塔(24)；
将来自第一脱乙烷塔进料筒(22)的顶部蒸气送至工艺气体压缩机(PGC)(26)；
在第二脱乙烷塔进料冷却器(28)中用丙烷，然后在第三脱乙烷塔进料冷却器(30)中用丙烯制冷剂，冷却来自PGC(26)的排出物(3)，并将该排出物送至第二脱乙烷塔进料筒(32)；
将来自第二脱乙烷塔进料筒(32)的液体(6)进料至脱乙烷塔(24)；
在冷箱(34)中冷却并部分地冷凝来自第二脱乙烷塔进料筒(32)的蒸气；
将来自冷箱(34)的工艺流出物在第一冷筒(36)中分离成气相(7)和液相；
在冷箱(34)中将来自第一冷筒(36)的液体蒸发，并将其循环至PGC(26)的第一级；
重新加热来自第一冷筒(36)的蒸气至成为富甲烷尾气产品；
在脱乙烷塔(24)中将乙烷和较轻的组分与C3和较重的组分分离；
在顶部脱乙烷塔冷凝器(40)中用丙烯制冷剂部分地冷凝顶部蒸气；
在脱乙烷塔回流筒(42)中，将来自顶部脱乙烷塔冷凝器(40)的工艺流出物分离成气相和液相，并将气相送至冷箱(34)，并将液体返回至脱乙烷塔(24)；
将脱乙烷塔底部液体(8)进料至C3分离器；和
冷箱(34)使来自第一冷筒(36)的尾气、PGC循环物流(12)、富C2物流(11)和进料至PDH反应器的丙烷进料过热，同时还使液体丙烯制冷剂过冷。
2.权利要求1所述的方法，其进一步包括在脱乙烷塔再沸器(38)中用丙烯制冷剂蒸气使脱乙烷塔底部液体再沸。
3.权利要求1所述的方法，其进一步包括在脱乙烷塔再沸器(38)中用淬火水使脱乙烷塔底部液体再沸。
4.权利要求1、2或3所述的方法，其进一步包括在脱乙烷塔上段上的泵循环，所述泵循环在脱乙烷塔第一泵循环冷却器(46)中使用丙烷、并在脱乙烷塔第二泵循环冷却器(48)中使用中级丙烯制冷剂，从而减少对顶部脱乙烷塔冷凝器(40)上的低级制冷剂的要求。
5.权利要求1、2或3所述的方法，其进一步包括将脱乙烷塔底部液体(8)进料至热泵式C3分离器，并将聚合物级丙烯与丙烷循环和C4+组分分离。
6.权利要求5所述的方法，其进一步包括将丙烷循环返回至脱丙烷塔，并将C4+与新鲜进料和丙烷循环分离。
7.权利要求5所述的方法，其中所述丙烷循环的一部分被作为侧馏分取自绕过所述脱丙烷塔的C3分离器。
8.一种用于从包括丙烷脱氢(PDH)反应器的PDH工艺回收丙烯的系统，所述系统包括：
工艺气体干燥器，其被配置为将干燥工艺气体(1)进料至第一脱乙烷塔进料冷却器(20)并用丙烷使其冷却；
第一脱乙烷塔进料筒(22)，其被配置为接收来自第一脱乙烷塔进料冷却器(20)的干燥工艺气体(2)；
脱乙烷塔(24)，其被配置为接收来自第一脱乙烷塔进料筒(22)的液体(4)；
工艺气体压缩机(PGC)(26)，其被配置为接收来自第一脱乙烷塔进料筒(22)的顶部蒸气；
第二脱乙烷塔进料冷却器(28)，其被配置为用丙烷冷却来自PGC(26)的排出物(3)；
第三脱乙烷塔进料冷却器(30)，其被配置为用丙烯制冷剂冷却来自PGC(26)的排出物；
第二脱乙烷塔进料筒(32)，其被配置为接收来自第三脱乙烷塔进料冷却器(30)的排出物，并将进料液体(6)送至脱乙烷塔(24)；
冷箱(34)，其被配置为接收、冷却和部分地冷凝来自第二脱乙烷塔进料筒(32)的蒸气；
第一冷筒(36)，其被配置为将来自冷箱(34)的工艺流出物分离成气相和液相，并将蒸发的液体循环至PGC(26)的第一级；
顶部脱乙烷塔冷凝器(40)，其被配置为用丙烯制冷剂部分地冷凝顶部蒸气；
脱乙烷塔回流筒(42)，其被配置为将来自顶部脱乙烷塔冷凝器(40)的工艺流出物分离成蒸气(7)和液体，将气相送至冷箱(34)；
管线(50)，其将来自脱乙烷塔回流筒(42)的液体导引至脱乙烷塔(24)；和
C3分离器，其被配置为接收来自脱乙烷塔(24)的底部液体(8)。
9.权利要求8所述的系统，其还包括脱乙烷塔再沸器(38)，所述脱乙烷塔再沸器(38)被配置为用丙烯制冷剂蒸气再沸脱乙烷塔底部液体。
10.权利要求8所述的系统，其还包括脱乙烷塔再沸器(38)，所述脱乙烷塔再沸器(38)被配置为用淬火水再沸脱乙烷塔底部液体。
CN202080075419.7A 2019-09-10 2020-09-10 用于从丙烷脱氢工艺回收丙烯的方法 Pending CN114616042A (zh)

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