CN101607694A - 氨合成用合成气的制备方法 - Google Patents
氨合成用合成气的制备方法 Download PDFInfo
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Abstract
一种用于制备适于制备氨的含氢和氮的合成气的方法,其中将通过天然气原料的转化获得的原料合成气(13)在深冷分离器(CS)中净化,并且将净化气(16)的一部分膨胀并用作同一分离器中的冷却介质,然后将所述膨胀的部分(16)再引入到净化合成气的主流中。还公开了根据本发明的合适设备以及常规设备的改造。
Description
技术领域
本发明涉及用于制备合成气(synthesis gas)或合成气(syngas)的方法和设备,所述合成气主要由氢和氮组成、适用于氨的合成。更具体地,本发明涉及一种方法和设备,其中所述合成气是通过烃例如天然气的转化和深冷精馏获得的。
背景技术
现有技术进行天然气蒸汽-转化,或蒸汽-甲烷转化(SMR),和/或通过空气的天然气原料的部分氧化,以获得适用于氨的合成,即主要含有摩尔比为约3∶1的H2和N2的合成气。在本说明书的其它部分中,术语HN比是指所述的H2/N2摩尔比。
现有技术的一个具体实施方案或形式主要包括以下方法:在空气引入与氨合成下游所需的氮的量相比过量的氮的情况下,在第一(初级)蒸汽转化器和第二转化器中转化,从而获得含H2和N2以及一定量的CO、CO2、Ar和H2O的原料合成气。通过在合适的深冷段中进行的深冷净化和HN比调节步骤将所述原料合成气净化,所述合适的深冷段有利地包括分馏塔,或冷却塔和回流冷凝器的组装体,或被称为Braun PurifierTM的净化器,或类似的已知装置。
在重要的方面中,所述净化和HN调节脱除杂质(CH4、Ar、H2O)和过量的氮。实际上,归因于第二转化器内部过量的空气,离开第二转化器的气体通常含一些氮余物(nitrogen excess)。过量的氮被脱除至将HN比平衡到氨合成所需的约3∶1的值所需的程度。将净化的合成气进料到主压缩机中,在所述主压缩机中将合成气的压力升高到适用于氨合成的值,通常100-200巴。
常规深冷净化方法基本上公开于US 3,572,046中,并且涉及原料合成气的自动制冷和膨胀,以提供深冷段的净制冷并且将整个深冷工艺保持在热平衡中。所述膨胀发生在气体膨胀器如汽轮机中,并且对保持深冷工艺运转是不可缺少的;然而,其包括在下游主合成气压缩机的吸入端处较低压力的缺点,从而增加用于新设备的所述压缩机的尺寸和成本。
在现有设备的改造中,通常希望增加合成气流量以及因而的设备的生产率。然而发现瓶颈在于起使总合成气流膨胀作用的原有膨胀器和相关管道的压力下降。还应当指出,膨胀的流通过深冷段中的热交换器,因而流的显著增加将需要新的且更大的膨胀器以及深冷段的昂贵改装。
世界上的许多SMR氨工厂,包括实施著名的Braun PurifierTM方法的那些,可以从改造干预(revamping intervention)和生产率增加中受益。因此,感到了克服上述缺点和限制的需要。
发明内容
本发明的问题在于通过天然气的蒸汽转化改善用于制备适用于氨合成的合成气的已知方法,特别涉及包括采用Braun PurifierTM技术的那些的现有氨设备的改造。具体地,本发明旨在减小与用于深冷净化工艺的净制冷的合成气膨胀有关的上述缺点。
该问题是通过一种用于制备适于制备氨的含氢和氮的合成气的方法解决的,所述方法包括以下步骤:
a)将烃原料转化,所述转化包括变换(shift)、CO2脱除和甲烷化的步骤,从而获得含H2、N2和杂质的原料合成气流;
b)将所述原料气流在深冷段中冷却至深冷温度并且进行净化和HN比调节处理,从而获得含摩尔比为约3∶1的H2和N2的净化合成气流;
c)将所述净化合成气流通过与所述冷却原料气流的热交换再加热,并且在主压缩段中压缩至适于氨合成的压力,其特征在于,在所述净化和HN比调节的步骤后,将处于深冷温度的所述净化合成气的较小部分分离并且进行膨胀,从而获得净化合成气的主流和较小的膨胀的流,并且将所述较小的流用作所述深冷段中的热交换介质,然后压缩并且在所述深冷段的出口和所述主压缩段上游与所述主流再合并。
在上述a)点的转化优选用蒸汽和空气进行,从而获得相对于3∶1的摩尔比具有过量的氮的原料合成气。烃原料通常为天然气。可以使用合成天然气(SNG)或另外的烃如石脑油。
术语深冷温度用于表示所述合成气的露点附近的温度,通常大大低于-100℃并且典型地为约-170℃(零下170度)。
以摩尔流量计,所述净化合成气的较小部分优选介于10和49%之间,更优选约15-30%。所述合成气的较小部分的优选膨胀率为约1.5至5.0。
根据本发明的另一方面,所述净化合成气的主要部分和较小部分分别与进入深冷分离器中的原料合成气进行热交换,以再加热处于环境温度附近的净化合成气,并且将原料合成气冷却至深冷温度,从而获得各自被再加热的合成气流,所述各自被再加热的合成气流在主合成气压缩段上游汇合。然后将较小部分在辅助压缩机中压缩以补偿之前的膨胀。
根据本发明的另一方面,通过在主热交换器中与净化合成气的膨胀的较小部分以及与净化合成气的剩余的主要部分的热交换,并且通过在优选为回流冷凝器的第二热交换器中与所述合成气的较小部分以及主要部分中的至少一个的热交换,使进入深冷段中的原料合成气在主热交换器中以及然后在所述第二热交换器中冷却。
所述两个热交换器被串联设置,即,第二热交换器在较深冷度工作。
在另外的实施方案中,将取自原料合成气的过量的氮液流用作制冷介质,使其在所述一个或多个热交换器中被再加热或至少部分蒸发。
因此,所述主热交换器和第二热交换器的制冷是由以下各项提供的:主净化合成气流的再加热、净化合成气流的膨胀的较小部分的再加热,以及可能的取自冷却原料合成气的冷凝的过量的氮的液流的再加热和部分或全部蒸发。
具体地,并且根据本发明的实施方案,以上列出的制冷流中的一个或多个可以绕过第二热交换器,被直接进料到主交换器中。在详细描述中给出了实施例。
在一个优选实施方案中,将原料合成气在主交换器中冷却到深冷温度,然后将其进料到接触装置如洗涤塔或分馏塔中;将来自所述接触装置的蒸汽在回流冷凝器中进一步冷却并且送到分离器中,在所述分离器中获得富氮液体回流流和净化合成气流;然后在所述分离器下游将净化气流分成较小部分和较大部分,所述较小部分被送到气体膨胀器中;然后使所述净化气的较小部分和较大部分平行通过所述回流冷凝器和主热交换器。最后,在环境温度附近,将较小气体部分在辅助循环压缩机中压缩并且与剩余的净化合成气汇合。
在优选实施中,主热交换器和回流冷凝器是深冷段内部的管或板式热交换单元,并且适于间接热交换。
转化优选通过以下方法进行:初级流转化,然后在适当的过量空气情况下的次级转化,随后是变换反应、CO2脱除和甲烷化的步骤。
本发明的另一个目的是用于制备适于制备氨的含氢和氮的合成气的设备,所述设备适于实现上述工艺。
更具体地,本发明的一个目的是一种设备,所述设备至少包括:
-烃转化装置,以及另外的用于变换反应、CO2脱除和甲烷化的装置,以提供含H2、N2和杂质的原料合成气流;
-深冷段,所述深冷段用于净化和精馏所述原料合成气流,适于将所述原料合成气转化成含摩尔比为约3∶1的H2和N2的净化合成气流;
-主压缩机,所述主压缩机配置用于接收来自深冷段的所述净化合成气流,并且适于将所述净化合成气的压力升高到适于氨合成的值;并且其特征在于,所述深冷段包括流送管,所述流送管取得处于深冷温度的所述净化气流的较小部分,并且将所述较小部分进料到膨胀器中,从而获得膨胀且进一步冷却的合成气流;所述深冷段还至少包括热交换器,所述热交换器适于通过与原料合成气的热交换将净化合成气的所述部分再加热,并且所述设备包括另外的压缩机,所述另外的压缩机配置用于在所述主压缩机上游将所述膨胀的较小合成气部分与剩余的净化合成气汇合。
在一个优选实施方案中,深冷段包括净化段,所述净化段又包括至少一个接触装置和蒸汽/液体分离器。接触装置例如为洗涤塔或反流冷凝器(分馏塔);分离器接收来自接触装置的蒸汽相并且向同一接触装置提供富氮液体回流流。
根据本发明的另一方面,使主要由过量的氮组成的取自所述接触装置的液流在膨胀阀中膨胀和冷却,并且进一步用作热交换介质将原料合成气冷却。在一个优选实施方案中,深冷段包括主热交换器和回流冷凝器,所述主热交换器和回流冷凝器进行进入深冷段中的原料合成气、来自所述膨胀器的净化合成气的较小部分、剩余的净化合成气的主要部分和膨胀的合成气流、以及获自所述液流的膨胀的流之间的热交换。在另外的实施方案中,制冷流中的一些可以绕过回流冷凝器。
本发明的另一个目的是常规设备的改造。具体地,本发明公开了一种改造用于制备含氢和氮且适用于制备氨的合成气的设备的方法,所述设备包括用于处理来自蒸汽转化装置的原料合成气的深冷段,所述改造方法特征在于提供手段用于取得在所述深冷段中处于深冷温度的净化气流的较小部分,将所述较小部分进料至气体膨胀器中,从而获得净化合成气的膨胀且进一步冷却的流,并且将所述流用作热交换介质以提供所述深冷段的净制冷。
根据本发明的方法和设备具有以下优点。
作为冷却介质的净化气的较小部分的使用允许获得离开次级转化器的气体流的有效深冷净化,因而将所述气流保持在高压,即无需使全部量的气体膨胀和再压缩。
另外的优点在于,从净化气流中分离并且用作深冷分离中的冷却介质的较小部分在净化步骤之后,即在深冷段下游与净化气流再合并。这避免了在深冷段入口处的流的稀释,并且使得深冷分离/净化更有效。较小部分与主净化流在深冷段下游的再合并具有另外的优点,即减小输入流;因此深冷分离器更小且较不昂贵。如果改造,则在不干预分离器的情况下可以达到较大的容量。
整个***令人惊讶地更有效率,对于相同量的膨胀气体,需要较少约30至60%的主合成气压缩机中的能量消耗,以及减少约20-30%的热交换区中的温度差。
本发明特别在使用现有技术方法操作的现有设备的改造方面具有优点,在所述现有设备中将全部净化气流膨胀以提供深冷段的净制冷。净化气流的较小部分的膨胀允许在无需较大的膨胀器和/或压缩机的情况下增加容量。
附图说明
图1是本发明的一个优选实施方案中的方法的示意性框图。
图2是根据本发明的方法和设备的一个优选实施方案的更详细的图。
图3至6是其它实施方案的图。
具体实施方式
参考图1,在基于转化的氨设备的前端中,将天然气原料10和蒸汽流51进料到初级蒸汽转化器50中,将由此获得转化气11送到进料有空气53的次级转化器52,并且产生原料合成气流12。所述合成气流12包含氢(H2)和氮(N2)以及杂质和惰性组分如碳氧化物类(CO、CO2)、水、氩、残余甲烷。
在一个优选实施方案中,次级转化器52在适当过量的空气的情况下工作,以在原料气12中获得与为了提供在下游氨合成单元入口处所需的H2/N23∶1摩尔比所需的氢的量相比过量的氮。所述原料气流12中过量的氮以摩尔计优选介于10%和50%之间,并且更优选等于15-30%。
然后根据基于转化的氨设备的标准构造,在段54中处理原料气流12,即将气体变换以将CO+H2O转化成H2和CO2,然后将CO2脱除,并且在甲烷转化器中将剩余的碳氧化物转化成甲烷。因为这些工艺步骤众所周知,所以没有详细显示。
将这样获得的干燥的、不含CO2的气体经由管线13进料到用于深冷净化和精馏的深冷(cryo)段CS。深冷段CS在图1中总体上由虚边界线表示,并且根据本发明的不同实施方案可以包括多个装置。具体地,净化段56包括在所述深冷段CS中,以通过分离包含冷凝的过量的氮以及较小量的冷凝的甲醇和氩的液流30而获得净化合成气14。
将原料合成气13冷却到深冷温度,例如约-170℃,以获得在所述净化段56中净化的冷却的流13a。将这样获得的净化合成气14分成主要部分14a和较小部分16,使较小部分16在典型地为汽轮机的气体膨胀器300中膨胀。归因于膨胀,所述部分16被进一步冷却,典型地约10℃。
将净化合成气主要部分14a和较小部分17用作深冷段CS中的热交换介质,并且分别作为流20和18离开深冷段CS,所述较小部分17取自膨胀器300。
在所示的实施方案中,使净化合成气的流14a和17平行且在深冷段CS的两个热交换单元中进行热交换,所述两个热交换单元即为将在下文中以更详细的方式公开的主热交换器和回流冷凝器。
气流18,即位于深冷段CS的出口的较小的净化合成气部分,在辅助压缩机201中被再压缩以恢复横跨膨胀器300的压降,并且与主流20汇合,以形成朝向主合成气压缩机200的输出流21。所述压缩机200通常是多级单元,其以22至100巴以上的高压流进料到氨段(未显示)中。
液流30还被用作深冷段中的热交换介质。由所述液流30的蒸发所导致的且含氮、甲烷和氩的流32也被深冷段CS排出并且典型地被用作燃料。
现在参考图2中显示的优选实施方案更详细地描述本方法。
深冷段CS的主要部件是:形成净化段56的主热交换器HE1、回流冷凝器HE2、接触装置57和液体/蒸汽分离器58,以及汽轮机-膨胀器300。该实施例中的接触装置57是洗涤塔,尽管可以使用反流冷凝器或“分馏塔”。
流13处的干燥的、不含CO2的进料气进入温度典型地介于0℃和40℃之间的深冷段CS。它在主热交换器HE1中被冷却到其露点或略低于其露点,以获得在约-170℃的流13a。
然后,冷却的流13a进入洗涤塔57。从分离器58向所述塔的顶部供给富氮液体回流流13d。来自塔57的塔顶馏出物蒸汽流13b在回流冷凝器HE2中被冷却,从而获得进入蒸汽/液体分离器58的冷却流13c。离开分离器58底部的液体形成上述回流流13d。将所述冷却流13c的温度调整到这样的水平,在所述温度水平,离开分离器58的净化蒸汽流14具有下游氨合成单元所需的接近3的H2∶N2摩尔比。取决于应用,流13c的温度通常为约-180℃。
所述净化合成气流14的大部分,典型地70至85%,形成主流14a,所述主流14a在回流冷凝器HE2中被加热成温度略低于流13b的温度的14b。然后流14b在主交换器HE1中被进一步加热,从而获得温度略低于来自转化器的原料气流13的温度的流20。这是来自深冷段CS的最终合成气产物的主要部分。典型地,流20具有介于20和40巴之间的压力,尽管可以使用更低或更高的压力。
离开洗涤塔57底部的包含冷凝的过量的氮和较少量的冷凝甲烷和氩的液流30通过阀59闪蒸至压力典型低于5巴,以获得闪蒸流31。然后引导所述闪蒸流31通过回流冷凝器HE2中的通道,在所述回流冷凝器HE2中的通道中,所述闪蒸流31通过被加热至略低于流13b温度的温度而部分蒸发成为流31a。然后此流31a通过主交换器HE1,在所述主交换器HE1中,流31a又达到略低于进料流13温度的温度。在深冷段的输出得到的流32典型地被用作工厂燃料。
因为如上所述的流14a和31在回流冷凝器HE2中的加热通常不足以提供流13b和13c之间所需的冷却,所以将净化合成气流14的较小部分16通到膨胀器300中,从而作为在典型地介于15巴和20巴之间的低压以及归因于本身膨胀而降低温度的流17离开。优选地,膨胀器300为汽轮机,以回收机械功W。
然后将此膨胀且进一步冷却的流17在冷凝器HE2中加热以获得温度略低于流13b的温度的流17a,从而完成HE2的热平衡。然后在主交换器HE1中进一步加热流17a以获得温度略低于进料流13的温度的流18,从而完成主热交换器HE1的热平衡。
如所示的,剩余的净化气流14的主要部分14a也通过冷凝器HE2和主热交换器HE1以获得主流20。
然后将膨胀且再加热的流18进料到辅助压缩机201,以恢复横跨膨胀器300的压降,并且重新加入主流20中,以形成流21,所述流21是所制备的可用于下游氨合成单元的合成气产物的全部的流(full flow)。流21典型地直接流到主合成气压缩机200,所述主合成气压缩机200产生用于下游氨合成单元的约100-200巴的高压流22。
应当指出,本发明通过使产物气(流14)的较小部分通过膨胀器300膨胀,在工艺方案中的最冷点处-热交换器HE2的冷侧上-提供额外的制冷,膨胀部分随后被加热到环境温度并且再压缩到产物气的主要部分中。
在图2中,通过再加热产物气的主要部分(从流14a到流14b)以及通过当流31穿过HE2变成流31a时流31的再加热和至少部分蒸发,还提供一些用于热交换器HE2的显著制冷。
现在示出图3至6的备选实施方案。在图3中,净化合成气流的部分14a绕过回流冷凝器HE2并且被直接送到热交换器HE1中。因此,由被加热成17a的流17,并且通过流31的再加热和部分蒸发提供对冷凝器HE2的制冷。
在图4的另外的实施方案中,流31绕过冷凝器HE2并且被送到主交换器HE1中,因此HE2的制冷由流14a和流17提供。
在图5的实施方案中,合成气流17绕过冷凝器HE2。
在图6的实施方案中,合成气流14a和液流31都绕过冷凝器HE2,使得HE2中的热交换在被再加热成17a的净化合成气部分17与被冷却成13c的原料合成气13b之间。
如上所述,本发明还涉及改造用于制备适用于氨合成的合成气的常规设备的方法,其特征在于以进行以上工艺的方式更改现有设备,具体而言,提供将净化合成气的较小部分16进料到膨胀器300、以及将流17进料到交换器HE2和HE1,或如图5中那样直接进料到HE1的流送管。
更具体而言,在用于制备合成气的设备中,所述设备除其它部件之外包括用于处理来自流转化器50、52和处理段54的原料合成气13的深冷段CS,本改造方法涉及至少提供流送管16,所述流送管16取得在所述深冷段CS中处于深冷温度的净化气流14的较小部分,并且将所述部分16进料到膨胀器300中,从而获得膨胀且冷却的净化合成气的流17,所述流17被用作热交换介质以提供所述深冷段的净制冷。在改造干预中,膨胀器300可以是原有(已有)膨胀器或新的膨胀器。
本发明易于应用到其它的合成气制备技术中,包括非标准合成气制备,比如气体加热对流转化器。在另外的实施方案中,在该工艺中可以不包括初级转化器。
Claims (14)
1.一种用于制备适于制备氨的含氢和氮的合成气的方法,其中:
-将烃原料(10)转化,所述转化包括变换、CO2脱除和甲烷化的步骤,从而获得含H2、N2和杂质的原料合成气流(13);
-将所述原料气流(13)在深冷段(CS)中冷却至深冷温度并且进行净化和HN比调节,从而获得含摩尔比为约3∶1的H2和N2的净化合成气流(14);
-将所述净化合成气流(14)在所述深冷段(CS)中再加热,然后在主压缩段(200)中压缩至适于氨合成的压力值,
其特征在于,在所述净化和HN比调节的步骤后,将处于深冷温度的所述净化合成气的较小部分(16)分离并且进行膨胀,从而获得主净化合成气流(14a)和较小的、膨胀的净化合成气流(17);将所述较小的流(17)用作所述深冷段(CS)中的热交换介质,然后压缩并且在所述深冷段(CS)的出口和所述主压缩段(200)上游与主流再合并。
2.根据权利要求1所述的方法,其中以摩尔流量计,所述净化合成气(14)的较小部分(16)介于10和49%之间,并且优选介于15和30%之间。
3.根据权利要求1或2所述的方法,其中所述净化合成气的较小部分(16)的膨胀具有介于1.5至5.0之间的膨胀率。
4.根据前述权利要求中的任一项所述的方法,其中将所述净化合成气的主要部分(14a)和较小部分(17)分别与进入所述深冷分离器的原料合成气(13)进行热交换,从而获得在所述主合成气压缩段(200)上游汇合的各个再加热的合成气流(20、18)。
5.根据前述权利要求中的任一项所述的方法,其中通过在主热交换器(HE1)中与所述净化合成气的膨胀的较小部分(17)以及与所述净化合成气的剩余的主要部分(14a)的热交换,并且通过在第二热交换器(HE2)中与所述合成气的较小部分以及主要部分中的至少一个的热交换,将所述原料合成气(13)在所述主热交换器(HE1)中以及然后在所述第二热交换器(HE2)中冷却。
6.根据权利要求5所述的方法,其中将所述原料合成气(13)在所述深冷段(CS)的主热交换器(HE1)中冷却至深冷温度,然后将它进料到接触装置(57)中;将来自所述接触装置(57)的蒸汽在回流冷凝器(HE2)中进一步冷却并且送到分离器(58)中,在所述分离器(58)中获得富氮液体回流流(13d)和净化合成气流(14);然后在所述分离器下游将所述净化气流分成较小部分(16)和较大部分(14a),所述较小部分(16)被送到膨胀器(300)中;然后使所述净化气的较小部分和较大部分平行通过所述回流冷凝器和主热交换器,并且通过主要与所述原料合成气流(13)的热交换再加热到环境温度附近;将所述较小气体部分在辅助循环压缩机(201)中压缩并且在所述合成气的主压缩机(200)上游与所述剩余的净化合成气汇合。
7.根据权利要求5或6所述的方法,其中在所述主热交换器(HE1)和任选地在所述第二热交换器(HE2)中,通过与取自所述原料合成气本身的过量的氮液流(31)的热交换,将所述原料合成气进一步冷却。
8.用于制备适于制备氨的含氢和氮的合成气的设备,所述设备适于进行根据权利要求1至7中的任一项所述的方法。
9.根据权利要求8所述的设备,所述设备至少包括:
-烃转化装置(50、52)以及用于变换反应、CO2脱除和甲烷化的合适装置,从而提供含H2、N2和杂质的原料合成气流(13);
-深冷段(CS),所述深冷段(CS)适于将所述原料合成气流(13)转化成含摩尔比为约3∶1的H2和N2的净化合成气流(21);
-主压缩机(200),所述主压缩机(200)配置用于接收来自所述深冷段的所述净化合成气流(21),并且适于将所述净化合成气的压力升高到适于氨合成的值;
并且其特征在于,所述深冷段(CS)包括流送管(16),所述流送管(16)取得处于深冷温度的净化气流(14)的较小部分,并且将所述较小部分进料到膨胀器(300)中,从而获得净化合成气的膨胀且进一步冷却的流(17);所述深冷段(CS)还包括至少一个热交换器(HE1、HE2),所述至少一个热交换器(HE1、HE2)进料有所述净化合成气的冷却的流(17)作为热交换介质,并且所述设备包括另外的压缩机(201),所述另外的压缩机(201)配置用于在所述主压缩机(200)上游将所述膨胀的较小部分(18)与所述剩余的净化合成气(20)汇合。
10.根据权利要求9所述的设备,其中所述深冷段(CS)包括净化段(56),所述净化段(56)又包括至少一个接触装置(57)和蒸汽/液体分离器(58),所述至少一个接触设备(57)进料有冷却的原料合成气(13a),所述分离器接收来自所述接触装置的蒸汽相(13c)并且对同一接触装置提供富氮液体回流流(13d)。
11.根据权利要求10所述的设备,其中将从所述接触装置取得的过量的氮液流(30)在膨胀阀(59)中膨胀并且冷却,并且用作热交换介质,以在所述深冷段(CS)中加热所述净化合成气并且冷却所述原料合成气(13)。
12.根据权利要求11所述的设备,其中所述深冷段(CS)包括用于冷却进入所述深冷段中的所述原料合成气(13)的主热交换器(HE1)和第二热交换器(HE2),并且其中,通过所述净化合成气的膨胀的较小部分(17),通过所述净化合成气的剩余的主要部分(14a)以及通过来自所述膨胀阀(59)的液流(31),将所述主热交换器(HE1)制冷,并且通过所述合成气较小部分(17)、合成气主要部分(14a)和液流(31)中的至少一个将所述第二热交换器(HE2)制冷。
13.根据权利要求12所述的设备,其中所述第二热交换器(HE2)是回流冷凝器。
14.一种改造用于制备含氢和氮且适于制备氨的合成气的设备的方法,所述设备包括用于处理来自转化装置(50、52、54)的原料合成气(13)的深冷段(CS),所述改造方法的特征在于,提供手段(16)用于取得在所述深冷段(CS)中处于深冷温度的净化气流(14)的较小部分,将所述较小部分进料至膨胀器(300)中,从而获得净化合成气的膨胀且进一步冷却的流(17),并且将所述流(17)用作热交换介质以提供所述深冷段的净制冷。
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CN102701235A (zh) * | 2012-07-02 | 2012-10-03 | 湖南安淳高新技术有限公司 | 一种三热交氨合成反应器 |
CN102985367A (zh) * | 2010-04-07 | 2013-03-20 | 阿梅尼亚·卡萨莱股份有限公司 | 从氨驰放气回收氢气和氮气 |
CN107514873A (zh) * | 2017-08-30 | 2017-12-26 | 浙江大学 | 一种合成气分离净化的装置及方法 |
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EP3026016A1 (en) | 2014-11-27 | 2016-06-01 | Casale SA | A method for revamping an ammonia plant |
CN105110291A (zh) * | 2015-07-21 | 2015-12-02 | 河南环宇石化装备科技股份有限公司 | 一种焦炉煤气回收制lng联产合成氨的方法 |
US9957161B2 (en) | 2015-12-04 | 2018-05-01 | Grannus, Llc | Polygeneration production of hydrogen for use in various industrial processes |
WO2019020513A1 (en) | 2017-07-25 | 2019-01-31 | Haldor Topsøe A/S | METHOD OF PREPARING A SYNTHESIS GAS |
US11124424B2 (en) * | 2017-07-25 | 2021-09-21 | Haldor Topsoe A/S | Process for the co-production of methanol and ammonia in parallel |
AU2018308587B2 (en) * | 2017-07-25 | 2023-12-07 | Haldor Topsøe A/S | Method for the preparation of ammonia synthesis gas |
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CN102701235A (zh) * | 2012-07-02 | 2012-10-03 | 湖南安淳高新技术有限公司 | 一种三热交氨合成反应器 |
CN107514873A (zh) * | 2017-08-30 | 2017-12-26 | 浙江大学 | 一种合成气分离净化的装置及方法 |
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