CN110394028A - 基于变压吸附与深冷分离耦合的大规模梯级空分装置 - Google Patents

基于变压吸附与深冷分离耦合的大规模梯级空分装置 Download PDF

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CN110394028A
CN110394028A CN201910667188.8A CN201910667188A CN110394028A CN 110394028 A CN110394028 A CN 110394028A CN 201910667188 A CN201910667188 A CN 201910667188A CN 110394028 A CN110394028 A CN 110394028A
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田一良
乔英云
田原宇
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China University of Petroleum East China
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Abstract

本发明提供一种基于变压吸附与深冷分离耦合的大规模梯级空分装置。空气加压风机出口与脱二氧化碳和干燥的径向预处理吸附塔组的入口相连，吹扫气的入口与径向预处理吸附塔组的出口相连，塔组出入口均装有切换预处理吸附塔的程控阀；径向变压吸附塔组的入口与径向预处理吸附塔组的出口通过程控阀，塔组出入口均装有程控阀，并在径向预处理吸附塔组的入口接有减压泵；径向变压吸附塔组的出口通过程控阀与压缩机联通，后面再依次连接换热器和低温精馏装置；减压泵通过换热器和吹扫气的入口相连，低温精馏装置的出入口安装有液氧泵和液氮泵；变压吸附塔组通过程控阀实现部分吸附塔吸附分离、部分吸附塔解吸再生循环使用。

Description

基于变压吸附与深冷分离耦合的大规模梯级空分装置
1.技术领域
本发明提供基于变压吸附与深冷分离耦合的大规模梯级空分装置，属于空气分离技术领域。
2.背景技术
现代煤化工、冶金工业、石油炼制和硫酸工业等生产需要消耗大量的氧气，而对氮气的需求量较小。现有氧气生产方法中，空气分离法是最经济的工业制氧方法。目前，在空气分离领域中，低温精馏法(深冷分离)是传统的制氧方法，变压吸附法和膜分离法是新兴的制氧方法。低温精馏法技术成熟、适宜于大规模生产高压氧气和高压氮气、能够得到高纯度的氧气和氮气，且回收率很高，但氧气和氮气产量比过小，仅有21：78(体积比)，难以满足高耗氧低耗氮的工业过程需要。变压吸附法技术较成熟，适宜于中小规模生产氧气、能够得到中等纯度的低压氧气，氮气低压排出，但由于氩气、氦气和氖气等惰性气体未能分离影响氧气纯度的进一步提高且回收率有待提高。膜分离法技术正在开发，适宜于小和超小规模生产氧气、能够得到低浓度的氧气，投资较高且尚无大规模工业化应用的分离膜。
为了降低投资，20世纪90年代从事低温工程设备开发的美国公司UniversityEnvirogentics Inc.(UEI)变压吸附和低温精馏耦合的新型制氧机。它利用变压吸附法的装置简单、结构紧凑、出氧时间快和低温精馏法的产品氧纯度高的优点，克服了低温精馏法需要消耗大量昂贵有色金属的缺点，投资为常规机组的2/3，能耗与常规机组相当。由于该制氧机将变压吸附装置设置在低温精馏的空压机和主换热器之间，经变压吸附装置所低压排出的氮气均经过空压机的压缩，所以变压吸附和低温精馏耦合后空压机的负荷和能耗未能降低，造成制氧能耗与常规机组相当。因此，急需开发大规模变压吸附-深冷分离复合的空气分离工艺和装备，满足现代工业对低压高纯度氧气的需求。
3.发明内容
为了克服现有空气变压吸附分离技术存在的不足，本发明的目的是开发一种基于变压吸附与深冷分离耦合的大规模梯级空分装置，该工艺能够显著降低高纯氧分离能耗和大规模制氧的投资以及昂贵有色金属材料的用量，实现了变压吸附分离和深冷分离的规模匹配，解决了变压吸附与深冷分离耦合的规模化难题，出氧时间快，氧氮产品比例调控方便。
本发明所采用的装置，利用径向变压吸附塔提高空气变压吸附分离的规模、降低分离能耗、降低出氧时间，实现了变压吸附分离和深冷分离的规模匹配；通过富氧空气低温精馏装置大幅度降低压缩机、精馏塔和主换热器的负荷，减少投资以及昂贵有色金属材料的用量，进一步降低高压高纯氧、氮气和惰性气体的分离能耗；利用变压吸附排出的低压氮气回收富氧空气压缩的余热，降低深冷分离的冷能消耗，同时解决了干燥和脱二氧化碳吸附塔的加热再生的吹扫气来源和热源，合理利用副产氮气，从而实现了对空气大规模、高纯度、低能耗的梯级分离和利用。
本发明的基于变压吸附与深冷分离耦合的大规模梯级空分装置特征是：空气加压风机出口与脱二氧化碳和干燥的径向预处理吸附塔组的入口相连，吹扫气的入口与径向预处理吸附塔组的出口相连，塔组出入口均装有切换预处理吸附塔的程控阀；径向变压吸附塔组的入口与径向预处理吸附塔组的出口通过程控阀，塔组出入口均装有程控阀，并在径向预处理吸附塔组的入口接有减压泵；径向变压吸附塔组的出口通过程控阀与压缩机联通，后面再依次连接换热器和低温精馏装置；减压泵通过换热器和吹扫气的入口相连，低温精馏装置的出入口安装有液氧泵和液氮泵；变压吸附塔组通过程控阀实现部分吸附塔吸附分离、部分吸附塔解吸再生循环使用。
在本发明中，径向预处理吸附塔组的吸附剂为沸石分子筛、活性氧化铝、活性炭、硅胶中的一种。
在本发明中，径向变压吸附塔组所用的吸附剂为5A分子筛、锂X型分子筛、锂A型分子筛、13X型分子筛及其碱土金属改性分子筛中的一种。
在本发明中，变压吸附分离装置为真空变压吸附或低压变压吸附。
在本发明中，径向变压吸附塔由塔壁、隔离筒和中心管由外向内依次按同心圆布置，隔离筒和中心管的顶部通过吸附剂压紧板形成吸附段上部封闭；塔壁与隔离筒形成上部封死的气室，隔离筒与隔离筒形成辅助吸附室，隔离筒与中心管形成吸附室，中心管内底部设置防死区导向锥筒；塔壁底部侧面连接切向进气口，吸附尾气出口连接中心管设置在塔顶部；塔壁、中心管和隔离筒与底板密封连接；辅助吸附室和吸附室底部分别安装辅助吸附剂卸料口和吸附剂卸料口。
在本发明中，变压吸附分离塔组得到的富氧空气浓度为30％-85％。
4.附图说明
图1为本发明的装置示意图。
附图标记说明
1.风机，2.脱水脱二氧化碳预吸附塔组，3.径向变压吸附塔组，4.减压泵，5.压缩机，6.程控阀，7.换热器，8.低温精馏装置，9.液氮泵，10.液氧泵。
下面结合图1和实施例来详述本发明的装置特点。
5.具体实施方式
以下实施例均按照图1所示的基于变压吸附与深冷分离耦合的大规模梯级空分装置。图1所述流程具体包括：
过滤后空气经过风机1加压后，通过脱水和脱二氧化碳吸附塔组2预处理后，干燥和脱二氧化碳的加压空气先通过径向变压吸附塔3吸附分离，30％-85％的富氧空气流出径向变压吸附塔组3，低压氮气作为中间产品；径向变压吸附塔组3通过程控阀6切换，达到饱和吸附的径向变压吸附塔被减压泵4通过降压解吸再生，待吸附的径向变压吸附塔吸附分离空气，实现径向变压吸附塔组3的循环使用；30％-85％富氧空气再经过富氧压缩机5加压到0.5-0.7MPa，用低压氮气通过换热器7换热后进入低温精馏装置8，分离得到液氧和液氮，经液氧泵10和液氮泵9加压、回收冷量和汽化后得到高压高纯的氧气和氮气；加热后的低压氮气用作径向预处理吸附塔组2的再生吹扫气，实现二氧化碳和水的吸附和解吸循环。
所述的径向预处理吸附塔组的吸附剂为沸石分子筛、活性氧化铝、活性炭、硅胶中的一种。
所述的径向变压吸附塔组所用的吸附剂为5A分子筛、锂X型分子筛、锂A型分子筛、13X型分子筛及其碱土金属改性分子筛中的一种。
所述的变压吸附分离装置为真空变压吸附或低压变压吸附。
所述的径向变压吸附塔由塔壁、隔离筒和中心管由外向内依次按同心圆布置，隔离筒和中心管的顶部通过吸附剂压紧板形成吸附段上部封闭；塔壁与隔离筒形成上部封死的气室，隔离筒与隔离筒形成辅助吸附室，隔离筒与中心管形成吸附室，中心管内底部设置防死区导向锥筒；塔壁底部侧面连接切向进气口，吸附尾气出口连接中心管设置在塔顶部；塔壁、中心管和隔离筒与底板密封连接；辅助吸附室和吸附室底部分别安装辅助吸附剂卸料口和吸附剂卸料口。
所述的变压吸附分离得到的富氧空气浓度为30％-85％。
实施例1
本实施例的预处理吸附剂为分子筛，变压吸附吸附剂为锂A型分子筛，变压吸附分离为真空变压吸附：
流程如下：
过滤后空气经过风机1加压后，通过脱水和脱二氧化碳吸附塔组2预处理后，干燥和脱二氧化碳的加压空气先通过径向沸石分子筛真空变压吸附塔3吸附分离，氮气被锂A型分子筛吸附，70％的富氧空气流出径向沸石分子筛真空变压吸附塔3；径向真空变压吸附塔组3通过程控阀6切换，达到氮气饱和吸附的径向真空变压吸附塔被减压泵4通过负压解吸再生，低压氮气作为中间产品，待吸附的径向真空变压吸附塔吸附氮气，70％的富氧空气流出，实现径向真空变压吸附塔组3的循环使用；70％的富氧空气再经过富氧压缩机5加压到0.5-0.7MPa，用低压氮气通过换热器7换热后进入低温精馏装置8，分离得到99％以上的液氧、液氮和惰性气体，经液氧泵10和液氮泵9加压、回收冷量和汽化后得到高压高纯的氧气和氮气；加热后的低压氮气作为径向预处理吸附塔组2的再生吹扫气，实现二氧化碳和水的吸附和解吸循环。
结果显示，实施例1的工艺中氧气纯度和回收率均大于99％；高压氮气纯度大于99％，回收率不到10％；相对低温精馏法氧气分离能耗降低25％，投资降低35％以上。
实施例2
本实施例的预处理吸附剂为分子筛，变压吸附吸附剂为5A型分子筛，变压吸附分离为低压变压吸附：
流程如下：
过滤后空气经过风机1加压后，通过脱水和脱二氧化碳吸附塔组2预处理后，干燥和脱二氧化碳的加压空气先通过径向沸石分子筛低压变压吸附塔3吸附分离，氮气被5A型分子筛吸附，70％的富氧空气流出径向沸石分子筛低压变压吸附塔3；径向低压变压吸附塔组3通过程控阀6切换，达到氮气饱和吸附的径向低压变压吸附塔被减压泵4通过降压解吸再生，低压氮气作为中间产品，待吸附的径向低压变压吸附塔吸附氮气，30％的富氧空气流出，实现径向低压变压吸附塔组3的循环使用；30％的富氧空气再经过富氧压缩机5加压到0.5-0.7MPa，用低压氮气通过换热器7换热后进入低温精馏装置8，分离得到99％以上的液氧、液氮和惰性气体，经液氧泵10和液氮泵9加压、回收冷量和汽化后得到高压高纯的氧气和氮气；加热后的低压氮气作为径向预处理吸附塔组2的再生吹扫气，实现二氧化碳和水的吸附和解吸循环。
结果显示，实施例2的工艺中氧气纯度和回收率均大于99％；高压氮气纯度大于99％，回收率不到60％；相对低温精馏法氧气分离能耗降低10％，投资降低15％以上。
本发明所提供的基于变压吸附与深冷分离耦合的大规模梯级空分装置，利用径向变压吸附塔使空气变压吸附分离规模成倍提高，可以达到30000m3/h以上，达到变压吸附分离和深冷分离的规模匹配的目的；通过富氧空气深冷分离有效降低了压缩机、精馏塔和主换热器的负荷，减少投资15％以上，降低昂贵有色金属材料的用量30％，进一步降低高压高纯氧、氮气和惰性气体的分离能耗；利用变压吸附排出的低压氮气回收富氧空气压缩的余热，降低深冷分离的冷能消耗，同时解决了干燥和脱二氧化碳吸附塔的加热再生的吹扫气来源和热源，合理利用副产氮气，从而实现了对空气大规模、低压、高纯度、低能耗的梯级分离和利用。

Claims (6)

1.基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，空气加压风机出口与脱二氧化碳和干燥的径向预处理吸附塔组的入口相连，吹扫气的入口与径向预处理吸附塔组的出口相连，塔组出入口均装有切换预处理吸附塔的程控阀；径向变压吸附塔组的入口与径向预处理吸附塔组的出口通过程控阀，塔组出入口均装有程控阀，并在径向预处理吸附塔组的入口接有减压泵；径向变压吸附塔组的出口通过程控阀与压缩机联通，后面再依次连接换热器和低温精馏装置；减压泵通过换热器和吹扫气的入口相连，低温精馏装置的出入口安装有液氧泵和液氮泵；变压吸附塔组通过程控阀实现部分吸附塔吸附分离、部分吸附塔解吸再生循环使用。
2.根据权利要求1所述的基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，径向预处理吸附塔组的吸附剂为沸石分子筛、活性氧化铝、活性炭、硅胶中的一种。
3.根据权利要求1所述的基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，径向变压吸附塔组所用的吸附剂为5A分子筛、锂X型分子筛、锂A型分子筛、13X型分子筛及其碱土金属改性分子筛中的一种。
4.根据权利要求1所述的基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，变压吸附分离塔组为真空变压吸附或低压变压吸附操作。
5.根据权利要求1所述的基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，径向变压吸附塔由塔壁、隔离筒和中心管由外向内依次按同心圆布置，隔离筒和中心管的顶部通过吸附剂压紧板形成吸附段上部封闭；塔壁与隔离筒形成上部封死的气室，隔离筒与隔离筒形成辅助吸附室，隔离筒与中心管形成吸附室，中心管内底部设置防死区导向锥筒；塔壁底部侧面连接切向进气口，吸附尾气出口连接中心管设置在塔顶部；塔壁、中心管和隔离筒与底板密封连接；辅助吸附室和吸附室底部分别安装辅助吸附剂卸料口和吸附剂卸料口。
6.根据权利要求1所述的基于变压吸附与深冷分离耦合的大规模梯级空分装置，其特征在于，变压吸附分离塔组得到的富氧空气浓度为30％-85％。
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