CN111107916B - 在异构化单元中使用顶部分隔壁 - Google Patents

在异构化单元中使用顶部分隔壁 Download PDF

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CN111107916B
CN111107916B CN201880060580.XA CN201880060580A CN111107916B CN 111107916 B CN111107916 B CN 111107916B CN 201880060580 A CN201880060580 A CN 201880060580A CN 111107916 B CN111107916 B CN 111107916B
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wall column
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M.巴加瓦
R.卡立塔
J.C.根特里
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Sulzer Management AG
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Abstract

本发明涉及一种组合的石脑油加氢处理（NHT）和异构化工艺方案，该方案包括分隔壁塔（DWC），该分隔壁塔置换多个蒸馏塔并且允许系统内优化的热集成。与常规方案相比，所公开的设计减少了资本成本和能量成本这两者。

Description

在异构化单元中使用顶部分隔壁
相关申请的交叉引用
本申请根据35 U.S.C. § 119(e)要求于2017年9月19日提交的美国临时专利申请序列号62/560,569的权益，其通过全文引用的方式并入本文，如同在本文中完整阐述一样。
技术领域
要求保护的本发明总体上涉及顶部分隔壁塔，并且更具体地但非限制性地涉及降低成本并提高效率的改进的异构化单元。
背景技术
异构化单元由于提供了一种升级传统的低辛烷值汽油调和料的简单工艺而对于精炼厂很重要。另外，精炼厂能够通过苯馏分的氢化来调节苯含量。如图1中所示，石脑油加氢处理（NHT）和异构化单元100由多个常规蒸馏塔构成。将来自NHT反应器的馈送流传送到第一稳定器塔102。第一稳定器塔102从馈送流中去除不可冷凝的组分作为废气。将稳定的底部产物流从第一稳定器塔102馈送到石脑油分流器塔104。石脑油分流器塔104将稳定的底部产物分离成轻石脑油顶部流和重石脑油底部流。
轻石脑油顶部流主要由C5-C6组分构成。通常，将轻石脑油顶部流馈送到脱异戊烷（deisopentanizer）塔106，该脱异戊烷塔106浓缩i-C5作为脱异戊烷塔106的顶部流。将剩余的C5-C6组分作为脱异戊烷塔106的底部流获得并馈送到异构化反应器108以进行辛烷值升级。在异构化之后，在第二稳定器塔110中进一步处理来自异构化反应器108的不稳定的异构体。随后，将轻烃在顶部流中作为废气去除，并且将稳定的异构体传送到脱戊烷塔112以去除浓缩的C5组分流。
将来自脱戊烷塔112的富含C5的流再循环回到上游的脱异戊烷塔106，以去除i-C5产物。将来自脱戊烷塔112的底部产物流馈送到脱异己烷塔114。将C6异构体产物流作为顶部流从脱异己烷塔114中去除，并且将重异构体产物流（主要是C7+馏分）作为底部流从脱异己烷塔114中去除。将富含n-C6的馏分作为侧馏分从脱异己烷塔114中去除，并再循环到异构化反应器。
图1的现有技术系统100具有若干缺点。现有技术系统100中的第一稳定器塔102和第二稳定器塔110在相对高的压力（在这种情况下分别为〜100 psig和〜160 psig）下操作。由于常规稳定器中使用的部分冷凝，在废气中的液体损失较高。类似地，石脑油分流器塔104也在高压（〜75 psig）下操作。因此，塔再沸器利用中等价格的中压（MP）蒸汽操作。
此外，由于涉及的塔的数量、在该工艺的各个阶段中观测到的典型的高操作温度和高操作压力，常规的异构化单元可为昂贵且耗能的操作。随着在精炼行业中对异构化单元的需求增加，期望改进工艺方案以使其成本更低且效率更高。
发明内容
分隔壁塔（DWC）技术使得能够提高传统异构化工艺方案的效率并且降低其成本。本发明的实施例涉及一种工艺，其中异构化用于获得用于汽油调和的高辛烷值C5和C6组分。本发明的实施例包括一种应用，其中利用DWC构思用较少数量的蒸馏塔置换多塔异构化配置。由于较低的塔操作压力和改进的系统内热集成的组合，DWC配置消耗的能量明显减少，并且降低了加热成本。
本发明的实施例涵盖加氢处理反应器稳定器塔，其中将第一稳定器塔和下游的石脑油分流器塔组合成单个顶部分隔壁塔（例如，参见图2和图3）。这种布置产生相似数量的产物，同时将塔的数量从两个减少到一个。新的混合塔在与常规稳定器相同的压力下操作。
在一些实施例中，DWC包括定位在DWC的顶部区段中以形成两个顶部半部的分隔壁，其中两个顶部半部用作独立的塔。例如，将图1的现有技术系统的第一稳定器塔和石脑油分流器塔组合成顶部分隔壁塔（例如，参见图2和图3）。在该特定的DWC中，流进入的DWC的一侧作为吸收器操作。贫石脑油流用作吸收介质。可从DWC塔的较重底部物或同一复合体内的其它附近塔中获得该贫石脑油流。DWC的另一侧像典型的蒸馏塔一样操作。因此，本发明的实施例涵盖此类塔，其中在同一塔内实行蒸馏和吸收两者。
类似地，也可将图1的现有技术系统的脱戊烷塔和脱异己烷塔组合成顶部DWC（例如，参见图2和图4）。对于该DWC塔，DWC的顶部部分表现为两个分离区域。一侧用作脱戊烷塔以去除C5组分，而另一侧作为脱异己烷塔操作以回收轻（主要是C6异构体）和重异构体（C7和更重）产物。
在一些实施例中，异构化稳定器在比图1的现有技术系统更低的压力下操作。例如，与图1的现有技术系统的第二稳定器塔的约160 psig相比，压力可为约75 psig。选择操作压力，使得与图1的现有技术系统相比，第二稳定器塔以较低温度加热设施（在这种情况下为低压蒸汽）操作。另外，通过与来自异构化反应器的反应器流出物底部物进行热集成，获得了对第二稳定器塔的一些再沸负荷。
在一些实施例中，包括第一稳定器塔和石脑油分流器塔的DWC也在高压（〜100psig）下操作。该布置补偿了下游第二稳定器塔的较低操作压力。在后一系统中损失的有价值的C5组分通过使用贫石脑油流进行吸收被捕获在上游DWC塔中。此外，由于温度较高，该布置便于与脱异戊烷塔进行热集成。
在一些实施例中，使用填充的闪蒸鼓，其中使用来自将第一稳定器塔和石脑油分流器塔组合的DWC塔的重石脑油底部物的一部分来汽提来自第二稳定器的废气。从鼓中以液体产物形式获得残留的贫石脑油流，并且该贫石脑油流在配置中用作吸收介质。
在一些实施例中，与图1的现有技术系统相比，通过将DWC技术应用于配置来利用低压（LP）和中压（MP）蒸汽的组合的该系统显著降低了设施成本。
附图说明
图1表示组合的石脑油加氢处理和异构化单元的现有技术系统；
图2表示根据本发明的实施例的用于在石脑油加氢处理和异构化单元中使用DWC技术的工艺方案；
图3表示根据本发明的实施例的用于顶部DWC稳定器/石脑油分流器设计的工艺方案；并且
图4表示根据本发明的实施例的用于顶部DWC脱戊烷塔/脱异己烷塔设计的工艺方案。
具体实施方式
本发明的实施例涉及异构化工艺，其中使用DWC技术将各个塔置换和/或组合在一起，目的是使设施消耗最小化。
现在参照图2，示出了异构化工艺方案200。方案200包括第一分隔壁塔（DWC）210和第二DWC 240。第一DWC 210包括顶部分隔壁211，该顶部分隔壁211将第一DWC 210的顶部部分212分隔成第一侧213和第二侧214。在图2中所示的实施例中，第一侧213被配置为作为稳定器塔操作，并且第二侧214被配置为作为石脑油分流器塔操作。在一些实施例中，第一侧213包括第一顶部区段215，并且第二侧214包括第二顶部区段216。第一冷凝器217联接到第一顶部区段215，并且被配置为冷凝从其接收的顶部物。可将来自第一冷凝器217的回流物馈送返回到第一顶部区段215。第二冷凝器218联接到第二顶部区段216，并且被配置为冷凝从其接收的顶部物。可将来自第二冷凝器218的回流物馈送返回到第二顶部区段216。底部再沸器219联接到第一DWC 210，并且被配置为接收来自第一DWC 210的底部流并且将加热的流返回到第一DWC 210的底部区段220。
第二DWC 240包括顶部分隔壁241，该顶部分隔壁241将第二DWC 240的顶部部分242分隔为第一侧243和第二侧244。在图2中所示的实施例中，第一侧243被配置为作为脱戊烷塔操作，并且第二侧244被配置为作为脱异己烷塔操作。在一些实施例中，第一侧243包括第一顶部区段245，并且第二侧244包括第二顶部区段246。第一冷凝器247联接到第一顶部区段245，并且被配置为冷凝从其接收的顶部物。可将来自第一冷凝器247的回流物馈送返回到第一顶部区段245。第二冷凝器248联接到第二顶部区段246，并且被配置为冷凝从其接收的顶部物。可将来自第二冷凝器248的回流物馈送返回到第二顶部区段246。底部再沸器249联接到第二DWC 240，并且被配置为接收来自第二DWC 240的底部流并且将加热的流返回到第二DWC 240的底部区段250。
用于方案200的示例性工艺流程通过将流230馈送到第一DWC 210的第一侧213开始。在图2的实施例中，第一侧213是稳定器，并且第二侧214是石脑油分流器。在一些实施例中，流230源自石脑油加氢处理反应器。第一侧213从流230去除不可冷凝的组分作为废气流231。稳定的底部产物从第一侧213下降并进入第二侧214。第二侧214将来自第一侧213的稳定的底部产物分离成轻石脑油顶部流232和重石脑油底部流233。
轻石脑油顶部流232主要由C5-C6组分构成。将轻石脑油顶部流232馈送到脱异戊烷塔251，该脱异戊烷塔251浓缩i-C5作为顶部流234。将剩余的C5-C6组分作为脱异戊烷塔251的底部流235获得，并且馈送到异构化反应器252，用于经由异构化反应进行辛烷值升级。在稳定器塔254中进一步处理来自异构化反应器252的含有不稳定的异构体的流236。将轻烃在顶部流237中作为废气去除，并且将含有稳定的异构体的流238传送到第二DWC 240的第一侧243，以去除浓缩的C5组分流。
在图2的实施例中，第一侧243是脱戊烷塔，并且第二侧244是脱异己烷塔。将富含C5的顶部流261从第二DWC 240的第一顶部区段245再循环到上游的脱异戊烷塔251，以去除i-C5产物。底部产物流从第一侧243下降并进入第二侧244。将C6异构体产物流262作为顶部流从第二DWC 240中去除，并且将重异构体产物流263（主要是C7+馏分）作为底部流从第二DWC 240中去除。将富含n-C6的流264作为侧馏分从第二DWC 240中去除，并将其再循环到异构化反应器252。
图3是图1的塔102和104与图2的第一DWC 210的并排比较。顶部分隔壁211将第一DWC 210的顶部部分212分离为第一侧213和第二侧214，即供参考的预分馏侧和产物侧。对工艺方案进行设计以去除不可冷凝的废气流231。另外，方案在另一侧将中沸点组分（C5-C7）浓缩为轻石脑油顶部流232，而在塔的底部处回收最高沸点组分（重石脑油）作为重石脑油底部流233。在顶部分隔壁211的馈送侧，贫石脑油流通过吸收减少了有价值的C5组分在废气中的损失。在顶部分隔壁211的产物侧上，中沸点C5-C7组分移动到顶部，并且高沸点组分向下移动。因此，该方案在同一塔内执行蒸馏和吸收的组合。此外，在吸收侧上的第一冷凝器217是部分水冷却冷凝器，而在蒸馏侧上的第二冷凝器218是使用空气冷却交换器的总冷凝器。
DWC 212在100 psig的高操作压力下操作，并且利用MP蒸汽作为底部再沸器219（例如，热虹吸再沸器）中的加热介质。塔的高温允许与在明显较低的压力下操作的下游脱异戊烷塔251的热集成。
脱异戊烷塔251是常规的蒸馏塔，其在顶部处去除异戊烷浓缩的流（顶部流234）。脱异戊烷塔251的再沸器利用LP蒸汽，而另一再沸器与来自上游DWC 212的热顶部C5-C7蒸气热集成。
图4是图1的塔112和114与图2的第二DWC 240的并排比较。第二DWC 240分离四股产物流：C5再循环流261、C6异构体流262和C7+流263以及n-C6再循环流264。在顶部分隔壁241的两侧上，两个总冷凝器247、248可用。在一些实施例中，冷凝器247、248是空气冷却交换器。在第二DWC 240的底部处的底部再沸器249利用LP蒸汽操作。
在本发明的实施例中，经由顶部蒸气产物管线上的压力控制器维持塔的顶部压力。预分馏侧具有来自顶部冷凝器的回流物。
下表1突出显示了方案200与现有技术系统100相比节省的能量和成本。
表1
Figure DEST_PATH_IMAGE002
下表2突出显示了方案200与现有技术系统100相比的操作参数。
表2
Figure DEST_PATH_IMAGE004

Claims (18)

1.一种异构化单元，包括：
- 第一分隔壁塔，包括：
被配置为稳定器塔的第一侧；和
被配置为石脑油分流器塔的第二侧；
第二分隔壁塔，包括：
被配置为脱戊烷塔的第一侧；和
被配置为脱异己烷塔的第二侧，
所述异构化单元进一步包括：
联接到所述第一分隔壁塔的脱异戊烷塔，所述脱异戊烷塔被配置为从所述第一分隔壁塔的所述第二侧接收轻石脑油顶部流；
异构化反应器，所述异构化反应器联接到所述脱异戊烷塔，并且被配置为从所述脱异戊烷塔接收底部流；和
稳定器塔，所述稳定器塔联接到所述异构化反应器，并且被配置为从所述异构化反应器接收包含不稳定的异构体的流，并将稳定的异构体馈送到所述第二分隔壁塔。
2.根据权利要求1所述的异构化单元，其中，所述第一分隔壁塔包括第一冷凝器和第二冷凝器，所述第一冷凝器被配置为将顶部流的一部分从所述第一分隔壁塔的所述第一侧回流到所述第一分隔壁塔的所述第一侧的顶部区段，并且所述第二冷凝器被配置为将顶部流的一部分从所述第一分隔壁塔的所述第二侧回流到所述第一分隔壁塔的所述第二侧的顶部区段。
3.根据权利要求1所述的异构化单元，其中，所述第二分隔壁塔包括第一冷凝器和第二冷凝器，所述第一冷凝器被配置为将顶部流的一部分从所述第二分隔壁塔的所述第一侧回流到所述第二分隔壁塔的所述第一侧的顶部区段，并且所述第二冷凝器被配置为将顶部流的一部分从所述第二分隔壁塔的所述第二侧回流到所述第二分隔壁塔的所述第二侧的顶部区段。
4.根据权利要求1所述的异构化单元，其中，所述第一分隔壁塔包括底部再沸器，所述底部再沸器被配置为从所述第一分隔壁塔接收底部流并将所述底部流的一部分馈送返回到所述第一分隔壁塔。
5.根据权利要求1所述的异构化单元，其中，所述第二分隔壁塔包括底部再沸器，所述底部再沸器被配置为从所述第二分隔壁塔接收底部流并将所述底部流的一部分馈送返回到所述第二分隔壁塔。
6.根据权利要求1所述的异构化单元，其中，所述第一分隔壁塔的所述第一侧和所述第二侧由顶部分隔壁分离。
7.根据权利要求1所述的异构化单元，其中，所述第二分隔壁塔的所述第一侧和所述第二侧由顶部分隔壁分离。
8.根据权利要求7所述的异构化单元，其中，所述第二分隔壁塔包括来自不含有所述顶部分隔壁的所述第二分隔壁塔的底部附近的位置的侧馏分。
9.根据权利要求1所述的异构化单元，进一步包括填充的闪蒸鼓，所述填充的闪蒸鼓联接到所述第一分隔壁塔并且被配置为接收来自所述第一分隔壁塔的底部流和来自稳定器塔的废气流，以产生贫溶剂，将所述贫溶剂馈送返回到所述第一分隔壁塔。
10.一种异构化方法，包括：
向第一分隔壁塔提供流，所述第一分隔壁塔包括被配置为稳定器塔的第一侧和被配置为石脑油分流器塔的第二侧；
经由较重烃流通过使用吸收来用所述第一分隔壁塔处理所述流，以便产生废气流；
用所述第一分隔壁塔处理所述流，以便利用所述第一分隔壁塔的所述第二侧产生轻石脑油顶部流；
将所述轻石脑油顶部流馈送到脱异戊烷塔；
用所述脱异戊烷塔处理所述轻石脑油顶部流；
将来自所述脱异戊烷塔的底部流馈送到异构化反应器，以便升级所述底部流的辛烷值；
将来自所述异构化反应器的不稳定的异构体流馈送到稳定器塔；
用所述稳定器塔处理所述不稳定的异构体流，以便产生稳定的异构体流；
将所述稳定的异构体流馈送到第二分隔壁塔；和
经由所述第二分隔壁塔产生包含C6异构体产物流的第一流和包含重异构体产物流的第二流。
11.根据权利要求10所述的方法，其中，所述第一分隔壁塔包括第一冷凝器和第二冷凝器，所述第一冷凝器被配置为将顶部流的一部分从所述第一分隔壁塔的所述第一侧回流到所述第一分隔壁塔的所述第一侧的顶部区段，并且所述第二冷凝器被配置为将顶部流的一部分从所述第一分隔壁塔的所述第二侧回流到所述第一分隔壁塔的所述第二侧的顶部区段。
12.根据权利要求10所述的方法，其中，所述第二分隔壁塔包括第一冷凝器和第二冷凝器，所述第一冷凝器被配置为将顶部流的一部分从所述第二分隔壁塔的所述第一侧回流到所述第二分隔壁塔的所述第一侧的顶部区段，并且所述第二冷凝器被配置为将顶部流的一部分从所述第二分隔壁塔的所述第二侧回流到所述第二分隔壁塔的所述第二侧的顶部区段。
13.根据权利要求10所述的方法，其中，所述第一分隔壁塔包括底部再沸器，所述底部再沸器被配置为从所述第一分隔壁塔接收底部流并将所述底部流的一部分馈送返回到所述第一分隔壁塔。
14.根据权利要求10所述的方法，其中，所述第二分隔壁塔包括底部再沸器，所述底部再沸器被配置为从所述第二分隔壁塔接收底部流并将所述底部流的一部分馈送返回到所述第二分隔壁塔。
15.根据权利要求10所述的方法，其中，所述第一分隔壁塔的所述第一侧和所述第二侧由顶部分隔壁分离。
16.根据权利要求10所述的方法，其中，所述第二分隔壁塔的所述第一侧和所述第二侧由顶部分隔壁分离。
17.根据权利要求16所述的方法，其中，所述第二分隔壁塔包括来自不含有所述顶部分隔壁的所述第二分隔壁塔的底部附近的位置的侧馏分。
18.根据权利要求10所述的方法，进一步包括将来自所述第一分隔壁塔的底部流和来自所述稳定器塔的废气流馈送到填充的闪蒸鼓以产生贫溶剂，将所述贫溶剂馈送返回到所述第一分隔壁塔。
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