CN1145774C - 低温精馏环形塔 - Google Patents

低温精馏环形塔 Download PDF

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CN1145774C
CN1145774C CNB991118855A CN99111885A CN1145774C CN 1145774 C CN1145774 C CN 1145774C CN B991118855 A CNB991118855 A CN B991118855A CN 99111885 A CN99111885 A CN 99111885A CN 1145774 C CN1145774 C CN 1145774C
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CN1243940A (zh
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Kk
K·K·王
���ֹ�ķ
J·F·比林哈姆
���ɿ������޹�˾
D·P·博纳奎斯特
B·阿曼
�¶���άϣ
R·F·德尔内维希
�ɳ��
M·M·沙
T·A·斯卡雷
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Abstract

环形塔，特别适用于低温精馏，它包括同轴取向的限定第一塔区的径向隔开的圆柱形塔壁，和两塔壁之间的第二塔区，其中在第一塔区和第二塔区的每个塔区中进行着不同流体混合物的精馏。

Description

低温精馏环形塔
本发明一般涉及精馏，尤其适用于低温精馏例如原料空气的低温精馏。
根据组分的相对挥发度将流体混合物分离成各个组份的精馏装置的主要投资是塔的壳体和塔所需要的空间的费用。当需要两个或多个塔进行分离时，情况尤其如此。在塔可以竖直叠放或并排设置时，低温精馏，例如原料空气的低温精馏常常使用这样的多塔系统。迫切需要有这样一种系统，这种系统能够在减少塔的投资和减少塔的所需空间情况下进行精馏。
因此本发明的目的就是提供一种精馏塔系统，与传统的系统相比较，这种精馏系统可减少塔的投资和降低空间要求。
上述的目的和其它的目的对于通过阅读本发明公开的本领域技术人员将是显而易见的，这些目的可通过本发明实现。本发明的一个方面是：
进行精馏的环形塔，该塔包括：
(A)限定第一塔区的圆柱形主塔壁；
(B)与主塔壁径向隔开的环形塔壁，在主塔壁和环形塔壁之间划分出第二塔区；
(C)将流体送入第一塔区的装置和将流体从第一塔区取出的装置；和
(D)将流体送入第二塔区的装置和将流体从第二塔区取出的装置。
本发明的另一方面是：
将原料空气进行低温精馏的设备，包括：
(A)高压塔和环形塔，该环形塔包括限定第一塔区的圆柱形主塔壁和与主塔壁径向隔开的环形塔壁，在主塔壁和环形塔壁之间划分出第二塔区；
(B)将原料空气送入高压塔的装置，将流体从高压塔送入第一塔区的装置，和将流体从第一塔区域送入第二塔区的装置；
(C)从第一塔区域至少回收产品氮和产品氧中之一种的装置；和
(D)从第二塔区回收产品氩的装置。
本发明的又一个方面是：
将原料空气进行低温精馏的设备，包括：
(A)包含限定低压区的圆柱形主塔壁的环形塔和该环形塔与主塔壁径向隔开，在主塔壁和环形塔壁之间划分出高压区；
(B)将原料空气送入高压区的装置，将高压区的流体送入低压区的装置；和
(C)从低压区至少回收产品氮和产品氧中之一种的装置。
本发明再一个方面是：
将原料空气进行低温精馏的设备，包括：
(A)低压塔和环形塔，该环形塔包括限定主塔区的圆柱形主塔壁和环形塔壁与主塔壁径向隔开，在主塔壁和环形塔壁之间划分出侧塔区；
(B)将原料空气送入主塔区的装置，将主塔区的流体送入低压塔的装置，和将低压塔的流体送入侧塔区的装置；和
(C)从侧塔区回收产品氧的装置。
本发明特别涉及以下几个技术方案：
1.进行精馏的环形塔，该塔包括：
(A)限定包括填料的第一塔区的圆柱形主塔壁；
(B)与主塔壁径向隔开的由主塔壁形成的空间内侧中的环形塔壁，在主塔壁和环形塔壁之间划分出第二塔区；
(C)将流体送入第一塔区的装置和将流体从第一塔区取出的装置；
(D)将流体送入第二塔区的装置和将流体从第二塔区取出的装置；
其特征是以由环形塔壁伸延到主塔壁的分离器限定相对于第一塔区的第二塔区的上端，和第二塔区包括环形塔盘。
2.进行原料空气低温精馏的设备，包括上述1所述的环形塔，还包括：
(A)高压塔；和
(B)将原料空气送入高压塔的装置，将流体从高压塔送入第一塔区的装置，和将流体从第一塔区送入第二塔区的装置；
其中将流体从第一塔区取出的所述装置包括从第一塔区回收产品氮和产品氧中的至少一种产品的装置，和将流体从第二塔区取出的装置包括从第二塔区回收产品氩的装置。
3.进行原料空气低温精馏的设备，包括上述1所述的环形塔，还包括：
(A)低压塔；
(B)将原料空气送入第一塔区的装置，将流体从第一塔区送入低压塔的装置，和将流体从低压塔送入第二塔区的装置；
其中将流体从第二塔区取出的所述装置包括用于从第二塔区回收产品氧的装置。
4.上述3所述的设备，还包括从第一塔区回收产品氮的装置。
本文所用的术语“产品氧”其含义指的是具有大于80％(摩尔)，优选地大于95％(摩尔)的氧浓度的流体。
本文所用的术语“产品氮”其含义指的是具有大于95％(摩尔)，优选地大于99％(摩尔)的氮浓度的流体。
本文所用的术语“产品氩”其含义指的是具有大于80％(摩尔)，优选地大于95％(摩尔)的氩浓度的流体。
本文所用的术语“塔”其含义指的是蒸馏塔或分馏塔或区，也就是说接触塔或区，在塔内液体相和蒸汽相逆流接触，例如通过蒸汽相和液体相在一系列的安装在塔内的竖直间隔的塔盘或塔板上和/或在填料元件例如结构填料或无规填料上的接触，以实现流体混合物的分离。为进一步讨论蒸馏塔，请参见R.H.Perry和C.H.Chilton主编的，纽约McGraw-Hill书籍出版公司出版的化学工程师手册，第五版，13节，连续蒸馏过程。
蒸汽和液体接触分离法取决于各组分的蒸汽压差。高蒸汽压(或者易挥发的或低沸点的)组分将易于在蒸汽相中浓集，而低蒸汽压(或难挥发的或高沸点的)组分将易于在液相中浓集。分凝是分离方法，籍此可以采用蒸汽混合物的冷却而将挥发性组分浓集在蒸汽相中，因此难挥发组分浓集在液相中。精馏或连续蒸馏是分离方法，该方法将蒸汽相和液体相逆流处理获得的逐级部分蒸发和冷凝结合起来。蒸汽相和液体相的逆流接触一般是绝热的，可能包括两相之间的积分的(分级的)或微分的(连续的)接触。使用精馏原理来分离混合物的分离方法装置常常互换地称为精馏塔、蒸馏塔或分馏塔。低温精馏是一种至少部分地在150°K或低于150°K的温度下进行的精馏方法。
本文用的术语“间接热交换”其含意指的是使两种流体进行热交换，而两流体彼此之间没有任何的物理接触或相互混合。
本文所用的术语“原料空气”其含义指的是主要包含氧气、氮气和氩气的混合物例如环境空气。
本文所用的术语“再沸器”其含义指的是能从塔的液体产生塔上升流蒸汽的热交换装置。
本文所用的术语“冷凝器”其含义指的是从塔蒸汽产生塔下降流液体的热交换装置。
图1是本发明的一个优选实施方案的示意图，其中在生产氩气的低温精馏系统中使用环形塔。
图2是图1所示的实施方案的较详细的视图。
图3是本发明另一个优选实施方案的示意图，其中在双塔型低温精馏系统中使用环形塔。
图4是本发明又一个优选实施方案的示意图，其中在侧塔型低温精馏系中使用环形塔。
图5是图4所示的实施方案的较详细的视图。
图中编号对于通用元件是相同的。
将参照各图详细说明本发明。图1和图2实例说明低温精馏系统的一个实施方案，其中可以应用本发明的环形塔。
现在参照图1和图2，原料空气1在压缩机2中被压缩，通过冷却器3冷却压缩热。然后加压的原料空气通过净化器4清除掉高沸点的杂质例如水蒸汽、二氧化碳和烃，净化器典型地是一个变温或变压吸附净化器。然后净化过的压缩原料空气5在初级热交换器6中通过与回流的间接热交换进行冷却。在图1所示的实施方案中，原料空气5的第一部分7通过增压压缩机8进一步被压缩，第二部分9通过增压压缩机10进一步被压缩，所得到的进一步被压缩的原料空气部分11和12和余下的压缩原料空气部分50通过初级热交换器6被冷却，以便分别在物流51、52和53中产生压缩的、净化的和冷却的原料空气。物流52通过涡轮膨胀机55涡轮膨胀形成物流54，以便为随后的低温精馏产生致冷，物流54然后送入环形塔24。物流51和53各自送入高压塔21。
在高压塔21内，原料空气通过低温精馏被分离成富氮蒸汽和富氧液体。富氮蒸汽以物流22送入再沸器23中，其中富氮蒸汽通过与环形塔24底部的液体的间接热交换而形成富氮液体25。富氮液体25的一部分26作为回流返回高压塔21，富氮液体25的另一部分27在热交换器6中进行过冷，然后作为回流送入环形塔24中。富氧液体由高压塔21的底部以物流28送入环形塔24中，富氧液体的一部分56送入氩气冷凝器29中，其中富氧液体通过与富氩蒸汽的间接热交换而被蒸发，所得到的富氧流以物流30所示由冷凝器29送入环形塔24中。富氧液体的另一部分57直接送入环形塔24中。
环形塔24包括圆柱形主塔壁70和与主塔壁径向隔开的圆柱形环形塔壁71。同心的圆柱形壁70和71限定了第一塔区72和第二塔区73。第二塔区73是主塔壁和环形塔壁之间的空间，第一塔区72至少包括主塔壁所包围的某些空间，但不包括第二塔区73的部分。第二塔区73利用分离器74在第二塔区73的上端与第一塔区72封闭隔离。第二塔区73在其下端通过分布板75与第一塔区72保持流体相通。正如图1和图2所示，在第二塔区73中，蒸汽/液体接触的内部构件优选是环形塔盘76。在第一塔区72中，蒸汽/液体接触的内部构件优选地包含填料。
主要含氧和氩的蒸汽由第一塔区72通过分布板75进入第二塔区73，在第二塔区，通过与下流液体的低温精馏，该蒸汽被分离成富氩蒸汽和富氧液体。富氧液体如物流箭头33所示通过分布板75而返回到第一塔区72。富氩蒸汽以物流34送入冷凝器29，其中富氩蒸汽如前所述，通过与蒸发富氧液体的间接热交换而被冷凝。所得到的富氩液体以物流35返回到第二塔区73而形成上述下流液体。一部分富氩液体36可以作为产品氩间接地从第二塔区73加以回收。另一种方案是，除了物流36之外，一部分富氩蒸汽可以作为产品氩直接从第二塔区73回收。
环形塔24是在低于高压塔21的压力下操作的。在环形塔24的第一塔区72中，进入第一塔区的各种原料利用低温逆流精馏被分离成富氮流体和富氧流体。富氮流体从环形塔24的上部作为蒸汽流37取出，经过初级热交换器6被加热，和作为产品氮38回收。废物流58从环形塔上部取出，经过热交换器6加热，和以物流59从系统中除去。富氧流体作为蒸汽和/或液体从环形塔24下部取出。如果作为液体取出，富氧液体可以用泵加压到高压，在作为高压产品氧回收前，既可以在单独的产品蒸发器中蒸发，也可以在初级热交换器6中进行蒸发。在图1所述的实施方案中，富氧流体作为液流39从环形塔24中取出，通过液泵60加压到高压，经过初级热交换器6被蒸发，作为产品氧被回收。液体氧的一部分61可以作为液体产品氧被回收。
图1和图2联合描述的系统中所使用的环形塔代替了常规的低温空气分离装置的低压塔和氩气侧塔。在图3所述的本发明的实施方案中，环形塔代替了常规的低温空气分离装置的高压塔和低压塔。图3所述的本发明的实施方案也包括类似于图1和图2对于生产产品氩联合描述的环形装置。可是，应该懂得，当实施图3所述的本发明的实施方案时，这样的产品氩的生产能力是不必要的，或者既使用常规的氩气体侧塔也可以提供这样的产品氩的生产能力。图3所叙述的系统的这些方面给予相同的编号，将不再进行详细讨论，因为系统的这些方面与前面图1和图2所述的系统联合讨论的方面相同。图3所例示的本发明环形塔与图1和图2所例示的环形塔不同之处在于，环形塔壁80在主塔壁81所限定的圆柱形空间的外部，和第二塔区82的压力高于第一塔区83，可是在图1和图2所述的实施方案中，环形塔壁在主塔壁限定的空间内，此外，第二塔区的压力大致和第一塔区的压力相同。
现在参照图3，原料空气流51和52送入第二塔区或高压塔区82，在高压塔区82中，原料空气通过低温精馏分离为富氮蒸汽和富氧液体。富氮蒸汽以物流84送入再沸器85，在再沸器中富氮蒸汽通过与第一塔区或低压塔区83底部液体的间接热交换冷凝形成富氮液体86。富氮液体86的一部分87作为回流返回到高压塔区82，它的另一部分88在热交换器6中过冷，然后作为回流送入低压塔83的上部。富氧液体由高压区82以物流89流出，一部分90流入冷凝器29，在冷凝器29中，富氧液体通过与富氩蒸汽的间接热交换而被蒸发，所得到的富氧流体由冷凝器29以物流30流入低压区83。富氧液体的另一部分91直接进入低压区83。
在低压区83内，各种不同的原料通过逆流低温精馏被分离为富氮流体和富氧流体。在图3所述的实施方案中，富氧流体从低压区83的下部以物流92取出。物流92的一部分93进入液体泵94中，由液体泵再进入再沸器85，在再沸器85中富氧流体通过与前述的冷凝的富氮蒸汽间接热交换而被蒸发。所得到的富氧蒸汽然后从再沸器85以物流95进入低压区83的下部。物流92的另一部分96通过液泵97加压到高压，通过初级热交换器6而被蒸发，作为产品氧98而被回收。液体氧的一部分99可以作为液体产品氧而被回收。
在图4和图5所述的本发明的实施方案中，采用环形塔以代替常规低温空气分离装置的侧塔和高压塔。
现在参照图4和图5，环形塔100具有限定第一塔区或主塔区102的圆形主塔壁101，和与主塔壁101径向隔开的环形塔壁103，将主塔壁101和环形塔壁103之间的第二塔区即侧塔区104划分开。环形塔壁103在主塔壁101限定的圆柱形空间内，侧塔区104的压力低于主塔区102。侧塔区104在其顶部利用分隔板105与主塔区102隔开，在侧塔区104底部利用分隔板106与主塔区102隔开。侧塔区104优选地含有作为传质内部构件的环形塔盘。
原料空气流51分为物流108和物流110，物流108送入低压塔109，物流110送入主塔区102。原料空气流12经过主热交换器6的局部通过，所得到的物流111通过涡轮膨胀机55进行涡轮膨胀，在图4所示的实施方案中，涡轮膨胀机直接与压缩机10耦联，并用于驱动压缩机10。所得到的涡轮膨胀原料空气流112然后由涡轮膨胀机55送入低压塔109。
原料空气流53送入热交换器113中，在热交换器113中，原料空气至少部分地冷凝，以物流114送入主塔区102。在主塔区102内，原料空气通过低温精馏被分离成富氮蒸汽和富氧液体。富氮蒸汽以物流115送入再沸器23中，在此再沸器中富氮蒸汽通过与低压塔109底部的液体的间接热交换而冷凝从而形成富氮液体116。如果需要的话，如图4所示，富氮蒸汽115的一部分117可以通过主热交换器6，并作为高压产品氮蒸汽而被回收。
富氮液体116作为回流送入主塔区102。如果需要，富氮液体116的一部分119可以作为高压产品氮液体被回收。富氧液体以物流120从主塔区102的下部取出，通过过冷器121进行过冷，所得到的过冷富氧液体以物流122所示，送入低压塔109。从主塔区102中取出的并含有氮、氧的液流123通过过冷器121过冷，然后作为物流124送入低压塔109的上部。
低压塔109操作压力低于主塔区102的压力。在低压塔109内，进入该塔的各种原料通过低温精馏被分离成含氮流体和含氧流体。含氮流体作为蒸汽流从低压塔109的上部取出，通过过冷器121和初级热交换器6被加热，以物流126从系统中除去。含氧流体以物流127从低压塔109的下部取出，送入侧塔区104，在侧塔区内，含氧流体通过逆流低温精馏分离为富氧流体和贫氧流体。贫氧流体作为从侧塔区104而来的蒸汽流128送入低压塔109的下部。一部分富氧流体作为液体流129从侧塔区104进入热交换器113，在该热交换器中富氧流体至少部分地通过与上述至少部分地冷凝的原料空气流53的间热接交换而蒸发，所得到的富氧流体以物流130由热交换器113回到侧塔区104。另一部分富氧流体以物流131作为液体从侧塔区104取出，通过液体泵132加压到高压，通过主热交换器6被蒸发，作为产品氧133被回收。液体氧流120的一部分134作为液体产品氧而被回收。
现在通过使用本发明，可以实现多组分混合物的精馏，而使用的空间和材料，特别是塔壳体材料，要比实现迄今为止等价的分离所需要的少。虽然参照某些优选的实施方案详细地说明了本发明，但是本领域的技术人员将会认识到，本发明还有其它的实施方案也是在本权利要求的精神和范围之内。例如，虽然参照低温精馏，例如空气精馏详细地讨论了本发明，但是应当懂得，可以应用本发明实现其它的精馏方法，例如石油分馏，烃分离和醇蒸馏。

Claims (4)

1.进行精馏的环形塔，该塔包括：
(A)限定包括填料的第一塔区的圆柱形主塔壁；
(B)与主塔壁径向隔开的由主塔壁形成的空间内侧中的环形塔壁，在主塔壁和环形塔壁之间划分出第二塔区；
(C)将流体送入第一塔区的装置和将流体从第一塔区取出的装置；
(D)将流体送入第二塔区的装置和将流体从第二塔区取出的装置；
其特征是以由环形塔壁伸延到主塔壁的分离器限定相对于第一塔区的第二塔区的上端，和第二塔区包括环形塔盘。
2.进行原料空气低温精馏的设备，包括权利要求1的环形塔，还包括：
(A)高压塔；和
(B)将原料空气送入高压塔的装置，将流体从高压塔送入第一塔区的装置，和将流体从第一塔区送入第二塔区的装置；
其中将流体从第一塔区取出的所述装置包括从第一塔区回收产品氮和产品氧中的至少一种产品的装置，和将流体从第二塔区取出的装置包括从第二塔区回收产品氩的装置。
3.进行原料空气低温精馏的设备，包括权利要求1的环形塔，还包括：
(A)低压塔；
(B)将原料空气送入第一塔区的装置，将流体从第一塔区送入低压塔的装置，和将流体从低压塔送入第二塔区的装置；
其中将流体从第二塔区取出的所述装置包括用于从第二塔区回收产品氧的装置。
4.权利要求3的设备，还包括从第一塔区回收产品氮的装置。
CNB991118855A 1998-08-05 1999-08-03 低温精馏环形塔 Expired - Lifetime CN1145774C (zh)

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DE69907822T2 (de) 2004-03-11
KR100442464B1 (ko) 2004-07-30
EP0978700B1 (en) 2003-05-14
DE69907822D1 (de) 2003-06-18
BR9904340A (pt) 2000-10-10
CA2279557C (en) 2003-03-18
CN1243940A (zh) 2000-02-09
CA2279557A1 (en) 2000-02-05
KR20000017038A (ko) 2000-03-25

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