CN100439838C - 一种节能空分装置 - Google Patents
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04624—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
- F25J3/0463—Simultaneously between rectifying and stripping sections, i.e. double dephlegmator
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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Abstract
本发明公开了一种节能空分装置,该装置包括精馏段、提馏段、换热器、空气过滤器、空气压缩机、预冷机组、分子筛纯化器、主换热器、冷凝器、节流阀、再沸器、透平膨胀器、第一粗氩塔、第二粗氩塔和精氩塔;本发明的节能空分装置与现有的低温空分装置的能耗相比,可节能30%以上,大大提高了能源的利用率,同时塔体高度可降低近一半,有利于设备安装维护、操作实施和操作安全。
Description
技术领域
本发明涉及空气分离技术领域,特别地,涉及一种节能空分装置。
背景技术
空分装置是对空气进行分离,并得到氧、氮、氩等高纯工业气体的装置,它被广泛应用于石油、化工、冶金、电子、能源、航空航天、食品饮料、医疗保健等各种工业领域。所得到的氧、氮和氩产品在一个国家国民经济中的应用十分广泛。其中,(1)氧气是地球上一切有生命的机体赖以生存的物质,它很容易与其他物质发生化学反应而生成氧化物,并产生和提供大量的热量,因此氧气可用于钢铁制造、化工工艺、金属加工、玻璃制造、石油回收和精炼、造纸、保健服务、航天国防等;(2)氮气的化学性质不活泼,在平常的状态下有很大的惰性,不容易与其他物质发生化学反应。因此,氮在冶金工业、石油回收和精炼、金属生产和加工、电子工业、化学工业中广泛地用来作为保护气体。液氮作为较方便的冷源,在食品工业、医疗事业、畜牧业、建筑以及科学研究等方面得到越来越广泛的应用;(3)氩气是目前工业上应用很广的稀有气体,其性质十分不活泼,在飞机制造、造船、原子能工业和机械工业部门,对铝、镁、铜及其合金和不锈钢时,往往用氩作为焊接保护气,同时在电子、照明行业,氩气亦有非常重要的应用。
自从上世纪70年代的两次“石油危机”以来,能源危机加深,强烈地要求许多领域能源的有效利用。在能耗很大的空气分离工业中,能源成本占了空气产品价格的75%。于是出现这样的情况,一方面,由于现代工业的发展,一些大型工业项目如钢铁工业、化学工业、石油开采等都需要由大型空分装置提供空气制品,需求量也越来越大。另一方面,能耗成本也随着能源危机,变得越来越大。因此在这样的形势下,提高空气分离技术的能量效率显得刻不容缓。空气分离设备生产厂也越来越注重对这方面开发研究。
在低温空分过程中,空分精馏塔是一个重要的传质单元操作过程,也是能耗最大的单元操作。流程中,大部分能量是用来完成精馏分离过程,仅有一小部分用来提供生产带压的气体产品或液体产品。在过去的20年中,由于空压机效率、净化技术、换热器效率和膨胀机技术方面的改进,使能耗降低了大约10~15%。这些经过改进的流程,在很大程度上降低了能耗,提高了产品的提取率,但是在空分精馏塔节能方面的进展却不大。
发明内容
本发明针对上述空分工业过程的高能耗问题,发明了一种节能空分装置,与传统空分装置相比能耗降低30~40%,大大提高了能源的利用率。
本发明采用如下的技术方案来实现本发明的目的:一种节能空分装置,该装置包括:精馏段、提馏段、换热器、空气过滤器、空气压缩机、预冷机组、分子筛纯化器、主换热器、冷凝器、节流阀、再沸器、透平膨胀器、第一粗氩塔、第二粗氩塔和精氩塔;其中,所述精馏段、换热器和提馏段依次平行相连,所述节流阀安装于精馏段的塔底液相导出管与提馏段的进料板之间,所述冷凝器安装于精馏段塔顶的产品导出管上,所述再沸器安装于提馏段塔底的产品导出管上;所述空气过滤器、空气压缩机、预冷机组、分子筛纯化器和主换热器依次相连后,连接到精馏段的底部;与主换热器相连的透平膨胀器连接到提馏段的中上部;第一粗氩塔、第二粗氩塔和精氩塔依次相连,第一粗氩塔连接到提馏段的中下部。
进一步地,所述的换热器为同心轴式换热器或板翅式换热器。
本发明的有益效果是,一种节能空分装置与现有的低温空分装置的能耗相比可节能30%以上,可以极大节省操作费用,因此,具有极大的经济效益和工业应用前景。另外由于空气精馏装置采用精馏段、换热器和提馏段依次平行相连的平行结构,使塔的高度大大降低,有利于设备安装维护、操作实施和操作安全。
附图说明
图1为本发明节能空分装置的流程结构图;
图2为传统的低温空气分离双级精馏塔的流程结构图;
图3为换热器的结构示意图,其中,(a)为同心轴式换热装置的结构示意图,(b)为板翅式换热装置的结构示意图;
图中:1-精馏段,2-提馏段,3-换热器,4-空气过滤器,5-空气压缩机,6-预冷机组,7-分子筛纯化器,8-主换热器,9-冷凝器,10-节流阀,11-再沸器,12-透平膨胀器,13-第一粗氩塔,14-第二粗氩塔,15-精氩塔,16-下塔,17-上塔,18-过冷器,19-主冷凝蒸发器。
具体实施方式
下面结合附图对本发明作进一步的说明,本发明的目的和效果将更加明显。
如图1所示,本发明的节能空分装置主要是由精馏段1,提馏段2,换热器3,空气过滤器4,空气压缩机5,预冷机组6,分子筛纯化器7,主换热器8,冷凝器9,节流阀10,再沸器11,透平膨胀器12,第一粗氩塔13,第二粗氩塔14,精氩塔15等组成。其中,精馏段1、换热器3和提馏段2依次平行相连,节流阀10安装于精馏段1的塔底液相导出管与提馏段2的进料板之间,冷凝器9安装于精馏段1塔顶的产品导出管上,再沸器11安装于提馏段2塔底的产品导出管上;空气过滤器4、空气压缩机5、预冷机组6、分子筛纯化器7和主换热器8依次相连后,连接到精馏段1的底部;与主换热器8相连的透平膨胀器12连接到提馏段2的中上部;第一粗氩塔13、第二粗氩塔14和精氩塔15依次相连,第一粗氩塔13连接到提馏段2的中下部。
换热器3(参见图3)可采用同心轴式(参见图3a)和板翅式(参见图3b)两种结构。其中,附图3a所示的同心轴式换热器中,精馏段1和提馏段2的流体分别走管程d和壳程D,或分别走壳程D和管程d,附图3b所示的板翅式换热器中,精馏段1和提馏段2的流体分别走板程和翅程,或分别走翅程和板程。冷凝器9和再沸器11在装置启动的时候开启,当装置在稳定操作条件下可以关闭。
原料空气经空气过滤器4过滤后进入空气压缩机5进行压缩,压缩空气出来后先经过预冷机组6,然后进入分子筛纯化器7,经纯化后的压缩空气分成两股,一股在通过主换热器8后进料到精馏段1的底部,另外一股在通过主换热器8后再经过一个透平膨胀器12进料到提馏段2的中上部,精馏段1为高压塔,经过精馏段1的初步分离,在精馏段1塔顶得到液氮LN2产品,在精馏段1塔底得到富氧液空,将富氧液空采出后经节流阀10回流到提馏段2上部,提馏段2为低压塔,最终在提馏段2塔顶得到高纯度的氮气GN2产品,塔底得到高纯度的气氧GO2和液氧LO2产品。为了挖掘精馏段1的精馏潜力,提高产品提取率,所以将部分空气直接引入提馏段2参与精馏。
精馏段1和提馏段2之间引入了换热器3,由于热耦合的存在,一些热量在两个部分之间传递,而这些热量恰恰可以用来产生对于精馏部分很必要的液相流和对于提馏部分很重要的气相流,此时,冷凝器9和再沸器11的热负荷都被大大降低,大量能量被再利用,从而大幅度地降低了精馏塔的能耗。
为了实现装置的平稳启动,引入冷凝器9和再沸器11,在装置启动的时候开启,当系统达到稳定状态以后可以关闭;本发明采用的冷凝器9和再沸器11额定功率比同等处理能力的传统精馏塔的冷凝器和再沸器的额定负荷至少小1~2倍。
从提馏段2中下部位氩富集区抽提部分氩馏分进入第一粗氩塔13继续精馏得到含氩95%以上的粗氩馏分。经第一粗氩塔13、第二粗氩塔14、精氩塔15分别去除其中的氧、氮组分后,在精氩塔的底部获得液氩LAr和气氩GAr产品。
从提馏段上部抽出部分污气氮作为循环气,经过空气压缩机5、预冷机组6、分子筛纯化器7、主换热器8后进入精馏段1,增加精馏段1回流比,有利于提高产品的纯度和提取率。
传统空分流程中空分精馏塔采用双级精馏塔技术,如图2所示,传统的低温双级精馏塔由下塔16、上塔17、过冷器18和主冷凝蒸发器19组成;而本发明的空分精馏塔采用一种节能空分塔,整个塔体也被分成了两个塔体,精馏段1和提馏段2,两个塔体被平行放置,并引入换热器3实现两个塔体之间的内部热交换,精馏段1、换热器3和提馏段2依次平行相连,大大的提高了能量的利用率,而且使塔的高度大大降低,有利于设备安装维护、操作实施和操作安全;另外,取消了过冷器18和主冷凝蒸发器19,具有显著的节能效果。
与传统的低温双级精馏塔相比,本发明的节能空分装置的连线上变化如下:进料方面,经过预冷、纯化后的压缩气体,通过主换热器8后分成两股,一股直接进料到精馏段1的底部偏上位置,另外一股在通过透平膨胀器后直接进入提馏段2的中上部位。出料方面,在精馏段1的顶部偏下位置引出并连接一个冷凝器9,得到液氮LN2产品,而在底部,富氧液经过一个节流阀到达提馏段的顶部偏下的位置。在提馏段2的底部引出,得到产品液氧LO2,为了装置的平稳启动连接了再沸器11,在底部偏下的位置引出并通过主换热器8冷量回收后,得到产品气氧GO2,在提馏段2的顶部引出并通过主换热器8后得到产品气氮GN2,顶部偏下的位置引出污氮气GwN2,并将部分污氮气连接至压缩机5前,增加装置的回流比。在提馏段2的中下部的位置侧提初氩馏分,经第一粗氩塔13、第二粗氩塔14、精氩塔15后,得到液氩LAr和气氩Gar产品。
本发明使空分主塔高压塔所必须的压力从常规的双级精馏塔下塔的610KPa,降低到本发明装置精馏段1的360kPa以下,节能近40%。同时,塔体高度下降近一半,有利于设备安装维护、操作实施和操作安全。
本发明提出的一种节能空分装置已通过较佳实施例子进行了描述,相关技术人员明显能在不脱离本发明内容、精神和范围内对本文所述的装置和操作方法进行改动或适当变更与组合,来实现本发明技术。特别需要指出的是,所有相类似的替换和改动对本领域的技术人员是显而易见的,它们都会被视为包括在本发明精神、范围和内容中。
Claims (2)
1.一种节能空分装置,其特征在于,该装置包括:精馏段(1)、提馏段(2)、换热器(3)、空气过滤器(4)、空气压缩机(5)、预冷机组(6)、分子筛纯化器(7)、主换热器(8)、冷凝器(9)、节流阀(10)、再沸器(11)、透平膨胀器(12)、第一粗氩塔(13)、第二粗氩塔(14)和精氩塔(15);其中,所述精馏段(1)、换热器(3)和提馏段(2)依次平行相连,所述节流阀(10)安装于精馏段(1)的塔底液相导出管与提馏段(2)的进料板之间,所述冷凝器(9)安装于精馏段(1)塔顶的产品导出管上,所述再沸器(11)安装于提馏段(2)塔底的产品导出管上;所述空气过滤器(4)、空气压缩机(5)、预冷机组(6)、分子筛纯化器(7)和主换热器(8)依次相连后,连接到精馏段(1)的底部;与主换热器(8)的原料空气管道相连的透平膨胀器(12)连接到提馏段(2)的中上部;第一粗氩塔(13)、第二粗氩塔(14)和精氩塔(15)依次相连,第一粗氩塔(13)连接到提馏段(2)的中下部。
2.如权利要求1所述的一种节能空分装置,其特征在于,所述的换热器(3)为同心轴式换热器或板翅式换热器。
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