CN107532819B - 反应器和加热器配置在石蜡脱氢工艺中的协同作用 - Google Patents
反应器和加热器配置在石蜡脱氢工艺中的协同作用 Download PDFInfo
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Abstract
提供了一种用于加热工艺流体的设备。该设备用于改善火焰加热器的占地面积和减小火焰加热器体积。该设备包括W形的工艺盘管以确保较小的单室火焰加热器以及具有较低轮廓的火焰加热器,从而提供相对于下游反应器定位的灵活性。
Description
优先权声明
本申请要求在2015年6月30日提交的美国临时申请No.62/186810的优先权,该申请的内容通过引用整体结合于此。
技术领域
本发明涉及用于包括化学反应的工艺中的火焰加热器,具体涉及重整工艺。
背景技术
火焰加热器是化工设备中的普通处理装置。火焰加热器将工艺物料流加热至反应温度,并且向具有吸热反应的工艺物料流供热。火焰加热器具有用于在外壳内部运送工艺流体的管的一般构型,其中使用燃烧器来燃烧燃料以加热管。
对于更复杂的工艺,并且对于化工设备中的工艺升级,需要新构型以减小火焰加热器所占用的面积,并且提供工艺流体的加热的新效率。
不同过程对火焰加热器具有不同需求,并且这些不同需求会影响生产具有显著经济效益的改进的火焰加热器的设计。
发明内容
本发明是一种改进的火焰加热器设计和与下游反应器的集成/整合/结合。
本发明的第一实施方案是一种用于重整系统的集成式设备,其包括:多个辐射式火焰加热器,所述辐射式火焰加热器具有配置在加热器内的至少一个工艺盘管、燃烧器和烟气出口,其中工艺盘管具有一个出口和至少一个入口;以及出口歧管,针对每个加热器配设一个出口歧管,所述出口歧管具有至少一个歧管出口和与工艺盘管出口流体连通的入口。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中每个工艺盘管具有采用平行取向的三个管的构型,其中两个半圆形的管状区段将所述三个管的端部连接,使得所述三个管和两个管状区段形成W形的盘管,其中,中心管具有增大/较大的直径,并且两个较小的管具有与入口端口连接的一个端部且较大的中心管具有与出口端口连接的一个端部。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,进一步包括对流管束,该对流管束具有加热管和与烟气出口流体连通的入口,其中加热管具有入口和出口。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中加热管用于蒸气发生/形成。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,进一步包括多个移动床反应器,其中针对每个反应器配设一个辐射式火焰加热器。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中反应器被沿竖向层叠,并且辐射式火焰加热器并排布置在反应器叠层的附近。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中工艺盘管入口端口和出口端口配置在火焰加热器的上表面上。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中烟气出口配置在火焰加热器的下表面上。本发明的一个实施方案是直至这一段中的第一实施方案的这一段中的一个、任一或所有在先实施方案,其中辐射式火焰加热器以并排布局布置。
本发明的第二实施方案是一种用于重整系统的集成式设备,其包括:多个移动床反应器,每个反应器都具有工艺流体入口和工艺流体出口;多个辐射式火焰加热器,其具有配置在加热器内的至少一个工艺盘管、燃烧器和烟气出口,其中工艺盘管具有采用平行取向的三个管的构型,其中两个半圆形的管状区段将所述三个管的端部连接,使得所述三个管和两个管状区段形成W形的盘管,其中,中心管具有增大/较大的直径,并且两个较小的管具有与入口端口连接的一个端部且较大的中心管具有与出口端口连接的一个端部;至少两个入口歧管,每个歧管都具有入口和多个出口,其中每个入口歧管出口与一个工艺盘管入口流体连通;以及出口歧管,针对每个加热器配设一个出口歧管,所述出口歧管具有与工艺盘管出口流体连通的入口和与反应器工艺流体入口流体连通的至少一个歧管出口。本发明的一个实施方案是直至这一段中的第二实施方案的这一段中的一个、任一或所有在先实施方案,其中反应器被沿竖向层叠,并且辐射式火焰加热器并排布置在反应器叠层的附近。本发明的一个实施方案是直至这一段中的第二实施方案的这一段中的一个、任一或所有在先实施方案,其中所述多个反应器包括沿竖向层叠的四个反应器。本发明的一个实施方案是直至这一段中的第二实施方案的这一段中的一个、任一或所有在先实施方案,其中工艺盘管入口端口和出口端口配置在火焰加热器的上表面上。本发明的一个实施方案是直至这一段中的第二实施方案的这一段中的一个、任一或所有在先实施方案,其中工艺盘管入口端口和出口端口配置在火焰加热器的上表面上。在一个替代实施方案中,烟气出口可以配置在火焰加热器的上表面或火焰加热器的下表面上。
本发明的第三实施方案是一种用于重整系统的集成式设备,其包括:多个反应器,每个反应器均具有工艺流体入口和工艺流体出口;多个辐射式火焰加热器,所述辐射式火焰加热器具有配置在加热器内的至少一个工艺盘管、燃烧器和烟气出口,其中工艺盘管具有包括至少两个管状区段的压缩式设计,其中每个管状区段均具有入口,并且管状区段汇合以形成具有一个出口的第三管状区段;以及出口歧管,针对每个加热器配设一个出口歧管,所述出口歧管具有与工艺盘管出口流体连通的入口和与反应器工艺流体入口流体连通的至少一个歧管出口。本发明的一个实施方案是直至这一段中的第三实施方案的这一段中的一个、任一或所有在先实施方案,其中每个工艺盘管均具有采用平行取向的三个管的构型,其中两个半圆形的管状区段将所述三个管的端部连接,使得所述三个管和两个管状区段形成W形的盘管,其中,中心管具有增大/较大的直径,并且两个较小的管具有与入口端口连接的一个端部且较大的中心管具有与出口端口连接的一个端部。本发明的一个实施方案是直至这一段中的第三实施方案的这一段中的一个、任一或所有在先实施方案,其中反应器是移动床反应器。本发明的一个实施方案是直至这一段中的第三实施方案的这一段中的一个、任一或所有在先实施方案,其中反应器是固定床反应器。本发明的一个实施方案是直至这一段中的第三实施方案的这一段中的一个、任一或所有在先实施方案,其中反应器沿竖向层叠,并且辐射式火焰加热器并排布置在反应器叠层的附近。
根据以下详细描述和附图,本发明的其它目的、优点和应用对本领域技术人员而言将变得显而易见。
附图说明
图1示出具有一个工艺盘管的火焰加热器的截面;以及
图2示出多个反应器和火焰加热器的一种布局。
具体实施方式
化学过程经常需要加热。工艺加热器被设计为将进料流或中间工艺物料流加热至工艺中的化学反应以合理速率发生所需的温度。工艺加热器可以是单室的或双室的,并且配备有允许加热工艺流体的像“U形”的不同形状盘管。盘管安装在包括燃烧器的火焰加热器中。火焰加热器通常是箱形炉,具有位于箱内的盘管和安装在炉的侧面或底部上的燃烧器。对于工业化过程而言,火焰加热器会是很大的物品。火焰加热器可达设备成本的25%,并且降低成本的设计改善很重要。
直接火操作的加热器通常引起非选择性的反应,例如烃的热转化或裂化。这些非选择性反应降低了产量并且增加了损失。重新设计的加热器可以减少这些损失并且适合更理想的建设成本、运行成本和加热器所需的减小的面积或较小的占用空间。
配置有U形工艺盘管的单室或双室火焰加热器和端壁安装式水平圆形火焰燃烧器广泛用于诸如脱氢和重整的工艺中。在脱氢工艺中,反应包括许多非期望的反应。估计30%至40%的非选择性由火焰加热器中的热裂化引起。除了降低建设费用和火焰加热器占据的覆盖范围或面积以外,加热器的重新设计还可以减少这些非选择性的反应的量。
本发明是一种用于多个反应器和辐射式火焰加热器的集成式系统。该设备可供用于向吸热过程增加热,其中反应器中的反应引起温度下降,并且工艺物料流在反应器之间被再加热以使反应达到期望反应温度。如图1所示的辐射式火焰加热器包括配置在火焰加热器10内的至少一个工艺盘管20。火焰加热器10包括燃烧器12和烟气出口14。设备100包括至少一个出口歧管30,该出口歧管30具有与每个工艺盘管出口22流体连通的入口32。出口歧管30包括用于使工艺物料流到达下游反应器的出口。
每个工艺盘管20具有基本上平行取向的三个管24的构型以及两个弯曲管状区段26,用以形成具有两个入口28和一个出口22的呈大致W形的工艺盘管。改进的工艺盘管20的使用允许更窄的火焰加热器。此外,W形盘管的使用允许使出口歧管更靠近火焰加热器工艺盘管出口。
在一个实施方案中,如图2所示的集成式设备包括多个移动床反应器50a、50b、50c、50d和多个辐射式火焰加热器10a、10b、10c和10d。移动床反应器50a、50b、50c、50d沿竖向叠置,并且催化剂向下流经一系列反应器床。工艺流体在进入各反应器50a、50b、50c、50d之前被加热,并从各反应器50a、50b、50c、50d离开以在再导入该系列中接下来的反应器50a、50b、50c、50d之前到达后续的火焰加热器10a、10b、10c、10d。在一个特定实施方案中,集成式设备包括4个反应器和4个火焰加热器,并且火焰加热器以并排布置配置。
通过重新设计火焰加热器10,加热体积减小并且加热器的宽度减小,并且火焰加热器10的占地面积或面积减小。在一个特定实施方案中,火焰加热器包括具有配置在火焰加热器的上表面上的入口端口和出口端口的工艺盘管。火焰加热器包括烟气出口,并且一个优选的实施方案包括配置在火焰加热器的下表面上的烟气出口。
在一个实施方案中,集成式设备包括对流管束。该对流管束是具有与火焰加热器的烟气出口流体连通的入口的单元。该对流管束包括对流管束内用于输送要加热的流体的加热管。该对流管束用于从以700℃与1100℃之间的温度离开火焰加热器的烟气回收热。一种热回收方法是使水通过加热管以产生蒸汽。
在另一实施方案中,该集成式设备用于重整系统。该重整系统包括多个反应器,其中每个反应器具有工艺流体入口和工艺流体出口。该设备还包括多个辐射式加热器,其中每个加热器具有配置在加热器内的至少一个工艺盘管。每个加热器包括燃烧器和烟气出口。每个工艺盘管具有采用平行取向的三个管的构型,其中两个半圆形的管状区段将这三个管的端部连接,使得所述三个管和所述两个管状区段形成W形的盘管,其中,中心管具有增大/较大的直径,并且两个较小的管具有与入口端口连接的一个端部且较大的中心管具有与出口端口连接的一个端部。该设备还包括至少两个入口歧管,其中每个入口歧管具有入口和多个出口,其中每个入口歧管出口与一个工艺盘管入口流体连通。该设备针对每个加热器包括一个出口歧管,每个出口歧管具有多个入口和与反应器工艺流体入口流体连通的歧管出口,其中每个入口与工艺盘管出口流体连通。在一个实施方案中,火焰加热器具有配置在火焰加热器的上表面上的工艺盘管入口端口和出口端口,以及配置在火焰加热器的下表面上的烟气出口。
反应器可以是移动床反应器或固定床反应器,其中一个优选实施方案使用移动床反应器。火焰加热器可以构造成被抬高或位于地面上以减小从出口歧管出口到反应器工艺流体入口的输送管线距离。
对于具有外部催化剂收集器的移动床反应器,反应器工艺流体入口通常位于反应器的底部。在本实施方案中,火焰加热器将处于标准高度/标高/基准高度(grade)处,其中,对流管束位于火焰加热器的侧方,或甚至位于火焰加热器的上方。出口歧管出口配置成最大限度地减小出口歧管出口与反应器工艺流体入口之间的高度差。
对于具有内部催化剂收集器的移动床反应器,反应器工艺流体入口通常位于反应器的顶部。在本实施方案中,辐射式火焰加热器被抬高以使得出口歧管出口可以处于与反应器工艺流体入口相同/相似的高度处。
虽然已使用目前被认为是优选实施方案的实施方案描述本发明,但是应理解,本发明不限于所公开的实施方案,而且旨在涵盖被包括在所附权利要求的范围内的各种改型和等同布置结构。
Claims (8)
1.一种用于重整系统的集成式设备,包括:
多个辐射式火焰加热器,所述辐射式火焰加热器具有配置在所述辐射式火焰加热器内的至少一个工艺盘管、燃烧器和烟气出口,其中所述烟气出口配置在所述辐射式火焰加热器的下表面上,其中所述工艺盘管具有一个出口和至少一个入口;以及
出口歧管,针对每个辐射式火焰加热器配设一个出口歧管,所述出口歧管具有至少一个歧管出口和与工艺盘管出口流体连通的入口。
2.根据权利要求1所述的集成式设备,其中,每个工艺盘管均具有采用平行取向的三个管的构型,其中两个半圆形的管状区段将所述三个管的端部连接,使得所述三个管和两个管状区段形成W形的盘管,其中,中心管的直径大于另外两个管的直径,并且直径较小的两个管具有与入口端口连接的端部且所述中心管具有与出口端口连接的端部。
3.根据权利要求1所述的集成式设备,还包括对流管束,所述对流管束具有加热管和与所述烟气出口流体连通的入口,其中所述加热管具有入口和出口。
4.根据权利要求3所述的集成式设备,其中,所述加热管用于蒸汽发生。
5.根据权利要求1所述的集成式设备,还包括多个移动床反应器,其中,针对每个反应器配设一个辐射式火焰加热器。
6.根据权利要求5所述的集成式设备,其中,所述移动床反应器沿竖向层叠,所述辐射式火焰加热器并排布置在反应器叠层的附近。
7.根据权利要求1所述的集成式设备,其中,所述工艺盘管的入口端口和出口端口配置在所述辐射式火焰加热器的上表面上。
8.根据权利要求1所述的集成式设备,其中,所述辐射式火焰加热器以并排布局布置。
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---|---|---|---|---|
CN101865450A (zh) * | 2010-06-08 | 2010-10-20 | 辽河石油勘探局总机械厂 | 海洋平台热采油燃油或燃气注汽锅炉 |
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4160701A (en) * | 1973-04-25 | 1979-07-10 | Linde Aktiengesellschaft | Tube furnace for the cracking of organic feed stock |
SU1511565A1 (ru) * | 1988-01-25 | 1989-09-30 | Всесоюзный научно-исследовательский и конструкторско-технологический институт компрессорного машиностроения | Двухсекционный теплообменник |
US4986222A (en) | 1989-08-28 | 1991-01-22 | Amoco Corporation | Furnace for oil refineries and petrochemical plants |
US5247907A (en) | 1992-05-05 | 1993-09-28 | The M. W. Kellogg Company | Process furnace with a split flue convection section |
RU2064823C1 (ru) * | 1994-07-13 | 1996-08-10 | Товарищество с ограниченной ответственностью - Научно-производственное объединение "Ленар" | Реактор с движущимся слоем катализатора |
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US5878699A (en) | 1998-02-05 | 1999-03-09 | The M. W. Kellogg Company | Process furnace |
US6178926B1 (en) | 1999-08-31 | 2001-01-30 | Foster Wheeler Corporation | Double-fired horizontal tube heater |
US6237545B1 (en) | 2000-04-07 | 2001-05-29 | Kellogg Brown & Root, Inc. | Refinery process furnace |
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US8490581B2 (en) | 2006-06-15 | 2013-07-23 | Exxonmobil Research And Engineering Company | Advanced fired heater unit for use in refinery and petro-chemical applications |
US8323365B2 (en) | 2007-05-22 | 2012-12-04 | Praxair Technology, Inc. | Dual mode reactor SMR integration |
US8282814B2 (en) | 2009-03-31 | 2012-10-09 | Uop Llc | Fired heater for a hydrocarbon conversion process |
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JP5608415B2 (ja) | 2010-05-10 | 2014-10-15 | 日精オーバル株式会社 | ガス燃焼ヒーター |
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WO2014025390A1 (en) | 2012-08-07 | 2014-02-13 | Foster Wheeler Usa Corporation | Method and system for improving spatial efficiency of a furnace system |
US9327259B2 (en) * | 2013-04-26 | 2016-05-03 | Uop Llc | Apparatuses and methods for reforming of hydrocarbons |
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