CN1301944C - 烯生产设备的制冷系统 - Google Patents

烯生产设备的制冷系统 Download PDF

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CN1301944C
CN1301944C CNB038080141A CN03808014A CN1301944C CN 1301944 C CN1301944 C CN 1301944C CN B038080141 A CNB038080141 A CN B038080141A CN 03808014 A CN03808014 A CN 03808014A CN 1301944 C CN1301944 C CN 1301944C
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refrigeration
refrigerant
compressor
cryogen
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CN1646455A (zh
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V·T·韦
Q·马
J·T·－C·吴
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CB&I Technology Inc
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Abstract

一种用于乙烯生产设备的制冷系统，该系统包括一种含有甲烷、乙烯和丙烯的闭合回路式三元制冷剂系统。将出自一个压缩机的三元制冷剂分离成级间排放物和压缩机末级排放物，从而产生富甲烷蒸气级份和两级富丙烯液体，以便在各个热交换级中得到不同的温度和不同程度的制冷，同时使流回至压缩机中的制冷剂组分保持基本不变，使总回流制冷剂的大部份流回第1级压缩机吸气口。该三元系统也可以用于使用高压脱甲烷塔的乙烯生产设备。

Description

烯生产设备的制冷系统
背景技术
本发明涉及一种可以满足烯生产设备的冷却要求的制冷系统。具体地说，本发明涉及一种三级或三元制冷剂的应用，这种制冷剂包括用于在乙烯生产设备中进行冷却的甲烷、乙烯和丙烯的混合物。
为从裂解加热器馏分中分离出所要求的产品，乙烯生产设备就需要制冷。通常使用丙烯和乙烯制冷剂。一般来讲，特别是在使用要求低温的低压脱甲烷塔的系统中，还要使用一个独立的甲烷制冷系统。因此，就需要三个从最低温度到最高温度串接起来的独立制冷系统。需要三个与吸气鼓、独立换热器、管道等配套的压缩机和驱动器系统。添加一个往复式或离心式甲烷制冷压缩机会部分抵消因使用低压脱甲烷塔所节省的资金成本。
几十年来，混合制冷剂系统在工业领域中是众所周知的。在这些系统中，在单一制冷系统中使用多种制冷剂，以提供温度范围较宽的制冷作用，这样就可以用一个混合制冷系统代替多级纯组分的串接制冷系统。发现这些混合制冷系统广泛用于以液化天然气为基本负荷的设备中。在美国专利US5979177中描述了一种两元混合制冷系统在乙烯设备中的应用，在该系统中制冷剂是甲烷与乙烯或与乙烷的混合物。但是，这种两元制冷系统相应于一个独立的丙烯制冷系统进行串接，使制冷温度范围达到-40℃或更高一些。因此，需要两个独立的制冷系统。
发明概述
因此，本发明的目的是提供一种用于烯生产设备的单一简单制冷系统，特别是用于使用低压脱甲烷塔的乙烯生产设备的制冷系统，该系统使用甲烷、乙烯和丙烯的混合物作为三元制冷剂。这种三元系统代替独立的丙烯、乙烯和甲烷制冷系统，这些系统用低压脱甲烷塔执行回收处理。本发明包括从压缩机级间排放物和末级压缩机的排放物中分离出三元制冷剂，分离成富甲烷蒸汽级份和两级富丙烯液体，从而在不同的热交换级中得到不同的温度和不同程度的制冷，同时使流回至压缩机的制冷剂成分基本保持不变，而且制冷剂总回流量的大部分回流到第一级压缩机吸气口。这样，根据热力学原理，使三元制冷剂系统能够优于对于独立制冷剂使用独立压缩机的系统，这种三元系统还可用于使用高压脱甲烷塔的乙烯生产设备，此时三元系统只提供丙烯和乙烯的制冷温度范围。在下面的描述中将使本发明的制冷系统的目的、布置和优点更加清楚。
附图说明
该图是用于说明本发明制冷系统的一个实施方案的部分乙烯生产设备的流程示意图。
优选实施方案的描述
本发明涉及一种烯生产设备，在该设备中首先对热解气体进行处理，以便除去甲烷和氢，然后用公知方法进行处理，以便产生乙烯以及丙烯和其他一些副产品，并将它们进行分离。下面结合一个主要用于生产乙烯的设备对该方法进行描述。通过低温冷凝和分馏对乙烯生产设备中的气体进行分离需要在一个比较宽的温度范围内进行制冷。乙烯生产设备的制冷系统中所花的资本成本可以占整个设备成本的很大部分。因此，节省制冷系统的资金将会对设备的整体成本有相当大的影响。
使用高压脱甲烷塔的乙烯生产设备的工作压力大于2.76Mpa(400psi)，塔顶温度通常在-85℃到-100℃之间。约为-100℃到102℃的乙烯制冷通常被用于冷却和产生塔顶回流液。一个使用工作压力低于约2.41Mpa(350psi)，通常为0.345-1.034Mpa(50-150psi)，塔顶温度在-110℃到-140℃之间的低压馏除器的乙烯生产设备要求甲烷温度级的制冷效果来产生回流。使用低压馏除器的好处在于所需要整体设备功率以及整体设备投资费用较低，而其不足在于需要更低的制冷温度，因此，除了乙烯和丙烯制冷系统之外，还必须有一个甲烷制冷系统。
本发明的三元制冷剂包括甲烷，乙烯和丙烯的混合物。根据乙烯设备的裂解原料、裂解难度和激冷系统压力以及其他条件可以改变这些成分的百分比，但通常的百分比为：甲烷为百分之7-20，乙烯为百分之7-30，丙烯为百分之50-85。对于使用低压脱甲烷塔的乙烯生产设备来讲，通常组成为：甲烷10％、乙烯10％和丙烯80％。使用三元制冷剂可以满足乙烯生产设备的所有制冷负荷及温度的要求，而不需要两个或三个独立制冷系统。
本发明的目的是提供所要求的制冷以从原料气体中分离出氢和甲烷，并为脱甲烷塔以及整个设备所需要的其他制冷提供进料。对于附图所描述本发明的具体实施方案，该实施方案适用于低压脱甲烷塔，三元制冷系统被布置为系列热交换器10，12，14，16，18和20，以提供用于乙烯生产设备所需的所有制冷等级。根据任一特定乙烯处理流程的具体要求，特别是根据具体原料气体的组成，可以将这些热交换器合并成更少单元，或是扩充成更多个单元。这些热交换器主要是散热片型热交换器，并且优选将它们组装在一个称作冷箱的绝热很好的结构中，以便防止热量增加，并使低温运行局限在局部。在描述三元制冷系统之前，仅仅是为了说明，先用具体温度作为例子对流过系统的原料气体进行描述。
加入的原料气体22是根据需要被调节和冷却过的热解气体，该原料气体的温度通常为15-20℃，压力一般约为3.45MPa(500psi)，通常是一种蒸汽流。原料气体中含有氢、甲烷和C2以及更高级组分包括乙烯和丙烯。原料气体22在热交换器10，12，14，16，18和20中被本发明的制冷系统逐渐冷却，同时进行合适的分离，产生脱甲烷塔的原料。原料气体22首先在热交换器10和12中在23处冷却到约-35℃。在热交换器14中，原料气体从-35℃冷到-60℃(在23处)。原料气体在热交换器16中从-60℃冷到-72℃，并在28处将流出物26中的冷凝液25分离出来。冷凝液25是用于脱甲烷塔(未示出)的下部原料。而剩下的蒸汽30在热交换器18中从-72℃冷到-98℃，并在36处将流出物34中的冷凝液32分离出来。冷凝液32是用于脱甲烷塔的中部原料。然后将蒸汽38在热交换器20中进一步从-98℃冷到-130℃，并在44处将流出物42中的冷凝液40分离出来。冷凝液40是用于脱甲烷塔的顶部原料。此后分离剩余蒸汽46(未示出)，从而产生氢流和低压甲烷流50。冷却回路52用于对低压脱甲烷塔的塔顶馏分进行冷却和部分冷凝，以便产生回流。出自脱甲烷塔的剩余塔顶馏分蒸汽形成高压甲烷流54。氢流48和低压甲烷流50以及高压甲烷流54在各热交换器中提供附加冷却。为了完成对原料气体流的描述，是含有C2和较重组份的脱甲烷塔的底部用来回收乙烯和丙烯以及其他成分。
除了原料气体流和三元制冷剂流以外，气流55，56，57和58是温度不同的不同乙烯生产设备气流，这些气流也通过各热交换器以便回收冷量。仅仅作为例子，气流55用于回收低压脱甲烷塔侧的再沸器的冷量。气流56回收脱乙烷塔进料和低压脱甲烷塔底部再沸器的冷量。气流57用于回收脱乙烷塔进料、乙烷再循环、乙烯蒸馏器侧再沸器和底部再沸器以及乙烯产品的冷量。最后的气流58回收低压脱乙烷塔进料、乙烯产品、乙烷循环以及在双压脱丙烷塔系统中消耗的制冷的冷量。
当温差较低时，可以在热流体和冷流体之间实现最大的传热效率。例如本发明提供的混合制冷剂在固定压力下，其温度随蒸汽的增加而增高，这与固定压力下在恒定温度时蒸发的纯组分制冷剂明显不同。因此，当方法的冷凝温度不变或相对不变时，纯组分制冷系统在冷却期间可能更有效，但当方法的冷凝温度下降时，则纯组分制冷系统在冷却期间的效率可能相对较低。对于本发明提供的混合制冷系统来讲，相关优点倒置了。
在乙烯生产设备中，某些要求制冷的冷却装置处于相对恒定的温度，而某些温度在下降。在未决的美国专利申请No.09/862253、申请日为2001年5月22日、发明名称为Tertiary Refrigeration Systemfor Ethylene Plants中描述了一种乙烯生产设备的混合制冷系统，该文献强调了在整个系统组成恒定。所以，发现恒定温度传热装置中的效率有些低。本发明旨在通过改变用于这些恒定温度传热装置的混合制冷剂的组成来提高混合制冷系统的效率。本发明特别涉及用于从乙烷中分离乙烯的制冷系统，该分离要求非常大的制冷效果。该原理也可以用于其它传热负荷低的恒温传热装置，例如脱乙烷塔。
对于本发明来讲，根据特殊的考虑在冷箱外控制乙烯蒸馏冷凝器59的总负荷。通常将壳管式热交换器用作乙烯分馏冷凝器的传热装置，当然也可以使用例如在冷箱中的散热片式热交换器。根据热力学知道，如果使用一个低压塔，则在一个所用的制冷系统中汽化曲线随温度倾斜时，对像乙烯分馏塔塔顶馏分、脱乙烷塔塔顶馏分以及脱丙烷塔塔顶馏分之类恒温处理气流的冷凝效果较低。宽的冷端温度差表明效率很低，并且造成三元制冷系统能量消费更高。对于脱乙烷塔冷凝器来讲，可以用乙烯分馏器侧的再沸器使用近似恒定的温度在两侧进行制冷。但是，对于乙烯设备中制冷消耗最大的乙烯分馏器冷凝器来讲，没有其他任何解决方法。为了制造能与使用独立压缩机的系统在能耗方面能竞争的三元系统，在本发明的三元系统中要求一种能接近传统丙烯制冷效果那样产生强制冷剂流的思路。
现在回到制冷系统本身，如上所述，三元制冷剂是甲烷、乙烯和丙烯的混合物，用多级制冷压缩机60压缩该三元制冷剂。在示例性实施方案中，有5个压缩级61，62，64，66和68，并有两个级间冷却器。级间冷却器70在第三级排气口72处，而级间冷却器74在第四级排气口76处。在冷却以后，将第四级排气口中的液体在鼓78中进行分离，以便得到重制冷剂80。鼓78中的剩余蒸汽82返回到第5压缩级68，并作为第5级的最终流出物84被萃取。该最终流出物84在冷却器86中冷却并部分冷凝，然后在鼓88中分离，经相分离后产生中间重量制冷剂90和轻制冷剂92。下面是压缩机的各典型工作条件和各工作条件的范围：
  吸气压力范围         典型吸气条件
  MPa   MPa   温度C
  第1级   0.011-0.016   0.014   -40
  第2级   0.4-0.55   0.46   9.0
  第3级   0.7-0.95   0.86   47
  第4级   1.1-2.0   1.5   37
  第5级   2.8-3.2   3.0   45
从鼓88出来的轻制冷剂通过所有热交换器10-20并在该过程中冷凝和过冷。在热交换器20的出口94处该制冷剂被过冷到约-130℃，然后经阀96闪蒸，得到最低制冷温度-140℃--145℃。这种制冷程度使42处的原料气流冷却到-130℃或更低，并在回路52中提供足够的冷却，从而由脱乙烷塔的塔顶馏份产生回流。
通常通过控制在气流988和100中的轻制冷剂的流量分别将气流26和34中的原料气体的温度控制在-72℃和-98℃。通常，由气流102提供的制冷可以满足热交换器20，18和16的制冷需要。轻制冷剂最后在热交换器14中过热到-45℃。当该轻制冷剂与部分重制冷剂和中间重量制冷剂混合以返回第一级吸气鼓104时，提供了所期望的过热温度5-15℃。
出自鼓88的液体90是中间重量制冷剂，该制冷剂在通过热交换器10，12和14时被过冷。利用阀106和108对所述过冷制冷剂进行闪蒸，该中间重量制冷剂就可控制23和24处的原料气体的温度。通过阀108，中间重量制冷剂经热交换器14和12回流，然后流回到用于压缩机第1级61的吸气鼓104。通过阀106，中间重量制冷剂经热交换器12和10回流，然后流回到用于压缩机第3级64的吸气鼓112。通过调节阀110和为热交换器10提供有限的制冷，以此来控制鼓88中的液位。然后将这部分中间重量制冷剂输送到用于压缩机第4级66的吸气鼓114。
出自鼓78的重制冷剂78约有88％是丙稀。该液体有两个主要作用，即冷却乙烯冷凝器59以及作为热交换器10中的主要冷源，从而使三元制冷系统保持自冷。从热交换器12出来的重制冷剂的过冷温度在116处为-10℃--35℃。下面的表简单说明了压缩机的吸气气流和压缩机的流量。
 压缩级   制冷剂类型   总流量的重量百分比   平均MW
 第1级吸气   100％轻制冷剂中间重量制冷剂重制冷剂   9.03.556.0
 第1级和第2级流量   68.5   38.14
 第3级侧入口   中间重量制冷剂   3.0
 第3级流量   71.5   38.14
 第4级侧入口   中间重量制冷剂   7.0
  重制冷剂   21.5
 第4级流量   100   38.48
 第5级进排气流量   轻制冷剂和中间重量制冷剂 22.5 34.45
如上表所示，为了节省能量，先将制冷剂分离，再将制冷剂重新组合，特别是在压缩机第1级中重新组合轻制冷剂和大部分重制冷剂以及某些中间重量制冷剂，使其在第一压缩级中占到总流量的大约70％，这样可以使压缩机轮稳定运行。由于在第1压缩级中占到总流量的70％，而且始终有比较均匀的摩尔重量，因此由第1级吸气鼓压力控制的叶轮正常速度同样适用于三元制冷剂压缩机，这与单一制冷剂压缩机系统一样。在从第4级气流中萃取重制冷剂以后，第5级中的流量和摩尔重量基本上变得更小。但是，可以设计第5级压缩，并且通过将气流重新循环到第一级可以控制负载变化，以便减少影响。对于控制流程中的冷却负荷来讲，可以使用的变量包括控制临界温度，调节整体制冷剂组成，调节分离鼓78和88的温度以及调节压缩机操作条件。
本发明的闭合回路式三元制冷系统带有从压缩机级间的一侧或多侧提取物，使得该系统成为一种通用系统，其中在该系统中可以形成不同的制冷剂组成，并可以提供不同的制冷能力。这使得可以用经济有效的方法来精确地控制温度。所以，只要单个闭合回路式三元制冷系统就足以为整个乙烯生产设备提供全部所需要的制冷，不论该乙烯生产设备使用低压脱甲烷塔还是高压脱甲烷塔均是如此，其能量消耗具有竞争力，而且整体设备成本也低。

Claims (4)

1.在从原料气体中生产烯的过程中利用制冷系统中的三元制冷剂对所述原料气体和其它烯生产过程中的流体进行冷却的方法，所述原料气体含有氢、甲烷、乙烯、其它C2以及更高级烃，其中用一个带有一系列热交换器的制冷系统冷却所述原料气体和其它烯生产过程中的流体，该方法包括如下步骤：
(a)在一个多级压缩机中压缩一种三元制冷剂蒸气，该制冷剂蒸气基本上由甲烷，乙烯和丙烯的选定混合物组成，所述多级压缩机有一个第1级和一个最末级以及至少一个中间级；
(b)从所述中间级的一个级中取出至少一部分所述的三元制冷剂蒸气；
(c)冷却所述三元制冷剂蒸气的被取出部分，以便形成剩余的三元制冷剂蒸气和一种重液体制冷剂，该重制冷剂中丙烯所占比率比所述选定混合物大；
(d)从所述剩余三元制冷剂蒸气中分离出所述重液体制冷剂，并将所述剩余三元制冷剂蒸气返送到所述最末级，而且使其通过该最末级；
(e)从所述压缩机的最末级萃取所述剩余三元制冷剂蒸气，将其冷却以使其一部分冷凝，由此形成一种中间重量的液体制冷剂，并使其未被冷凝部分形成一种轻蒸汽制冷剂；
(f)将所述重液体制冷剂、中间重量的液体制冷剂和所述轻蒸气制冷剂引入热交换器进行相互接触，而且使它们与所述原料气体以及其它烯生产过程中的流体在所述系列热交换器中接触，由此冷却所述原料气体以及其它烯生产设备过程中的流体，而加热并蒸发所述重液体制冷剂和中间重量的液体制冷剂，所述轻蒸气制冷剂首先被冷却并至少部分冷凝，然后使该轻蒸气制冷剂蒸发；和
(g)将所述轻、中和重的已蒸发的制冷剂返送到所述压缩机。
2.根据权利要求1的方法，其中从所述中间级的一个级中取出至少一部分所述三元制冷剂蒸气的步骤包括从所述级中取出所述全部三元制冷剂蒸气。
3.根据权利要求2的方法，其中所述中间级的所述一个级是倒数第2级。
4.根据权利要求1的方法，其中所述选定混合物含有50-85％丙烯。
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JP4339130B2 (ja) 2009-10-07
BR0309096A (pt) 2005-02-09
ZA200406617B (en) 2005-11-30
CN1646455A (zh) 2005-07-27
KR20050000382A (ko) 2005-01-03
US6637237B1 (en) 2003-10-28
US20030192341A1 (en) 2003-10-16
WO2003087022A1 (en) 2003-10-23
EP1492748B1 (en) 2010-05-19
CA2478632C (en) 2008-11-18
CA2478632A1 (en) 2003-10-23
EP1492748A1 (en) 2005-01-05
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KR100683442B1 (ko) 2007-02-20
AU2003223522A1 (en) 2003-10-27

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