CN102980023B - 一种液氨的汽化方法 - Google Patents

氨的汽化热为327. 3千卡/千克。

在工业生产中，氨汽化需要吸收大量热量。

当汽化产气量偏离设计值时，氨气汽化器 ... CN102980023B-一种液氨的汽化方法 -GooglePatents 一种液氨的汽化方法 DownloadPDF Info Publicationnumber CN102980023B CN102980023B CN201210476489.0A CN201210476489A CN102980023B CN102980023B CN102980023B CN102980023B CN201210476489A CN201210476489A CN201210476489A CN102980023B CN102980023B CN102980023B Authority CN China Priorartkeywords ammonia reboiler vaporizer heatexchange heatingagent Priorartdate 2012-11-21 Legalstatus(Thelegalstatusisanassumptionandisnotalegalconclusion.Googlehasnotperformedalegalanalysisandmakesnorepresentationastotheaccuracyofthestatuslisted.) Active Applicationnumber CN201210476489.0A Otherlanguages English(en) Otherversions CN102980023A (zh Inventor 杨建明 吕剑 赵锋伟 马辉 张伟 庞国川 石磊 CurrentAssignee(Thelistedassigneesmaybeinaccurate.Googlehasnotperformedalegalanalysisandmakesnorepresentationorwarrantyastotheaccuracyofthelist.) XianModernChemistryResearchInstitute OriginalAssignee XianModernChemistryResearchInstitute Prioritydate(Theprioritydateisanassumptionandisnotalegalconclusion.Googlehasnotperformedalegalanalysisandmakesnorepresentationastotheaccuracyofthedatelisted.) 2012-11-21 Filingdate 2012-11-21 Publicationdate 2014-10-15 2012-11-21 ApplicationfiledbyXianModernChemistryResearchInstitute filed Critical XianModernChemistryResearchInstitute 2012-11-21 PrioritytoCN201210476489.0A priority Critical patent/CN102980023B/zh 2013-03-20 PublicationofCN102980023A publication Critical patent/CN102980023A/zh 2014-10-15 Applicationgranted granted Critical 2014-10-15 PublicationofCN102980023B publication Critical patent/CN102980023B/zh Status Active legal-status Critical Current 2032-11-21 Anticipatedexpiration legal-status Critical Links Espacenet GlobalDossier Discuss QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemicalcompound 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FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 2 GTLACDSXYULKMZ-UHFFFAOYSA-N Pentafluoroethane Chemicalcompound 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CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1 238000005057 refrigeration Methods 0.000 description 1 Abstract 本发明公开了一种液氨的汽化方法。

主要解决液氨气化导致设备出现水击现象、换热管外表结霜，换热效率降低的问题。

将加热蒸汽通过蒸汽口进入再沸器管程，经换热管换热后加热再沸器内的热媒，蒸汽冷凝生成的水流出再沸器；热媒受热汽化，经换热后成为热媒气体，并上升至汽化器内，热媒气体加热汽化器管程，与汽化器管程内的氨换热后冷凝成热媒液，再流入再沸器内；液氨进入汽化器管程，接受热媒气体提供的热量后汽化成气态氨，气态氨通过汽化器管程出口排出。

Description 一种液氨的汽化方法 技术领域 [0001]本发明属于化工技术领域，具体涉及一种液氨的汽化方法。

背景技术 [0002]工业液氨转变为气态氨的过程，广泛应用于化工装置、制冷、热处理等行业。

胺化反应中经常使用气态氨，氨气主要是通过液氨经加热器加热液氨，使之汽化，保持所需要的压力。

[0003]现有技术中，液氨汽化分别由电加热制热水供汽化器提供热源，由汽化器将工业液氨进行汽化。

氨的汽化热为327.3千卡/千克。

在工业生产中，氨汽化需要吸收大量热量。

当汽化产气量偏离设计值时，氨气汽化器会出现严重水击现象。

当蒸汽或热水循环不足时，空气中的水受冷结霜于氨气加热器换热管外表，换热的热阻大增，换热效率降低。

同时，氨汽化器的换热管内外温差较大，设备容易产生疲劳，操作安全性差，受蒸汽压力波动时，氨气压力输送不稳定，较难连续稳定操作。

发明内容 [0004]针对背景技术存在的缺陷或不足，本发明的目的在于，提供一种液氨汽化方法，该方法能够消除设备水击现象，氨气压力输送稳定，且能连续稳定操作。

[0005]为了实现上述任务，本发明采取如下的技术解决方案： [0006]-种液氨的汽化方法，采用的设备包括相连通的再沸器和汽化器，其特征在于，按以下步骤操作： [0007]1)将加热蒸汽通过蒸汽口进入再沸器管程，经换热管换热后加热再沸器内的热媒，蒸汽冷凝生成的水流出再沸器； [0008]2)热媒受热汽化，经换热后成为热媒气体，并上升至汽化器内，热媒气体加热氨汽化器管程，与氨汽化器管程内的氨换热后冷凝成热媒液，再流入再沸器内； [0009]3)来自外界的液氨进入汽化器管程，接受热媒气体提供的热量后汽化成气态氨，气态氨通过汽化器管程出口排出，通过调节阀门直接控制氨气体流量和压力，并与蒸汽调节阀门形成控制回路，间接控制再沸器的换热量，维持氨气连续稳定排出。

[0010]上述热媒可以是二甲氧基甲烷、甲醇、乙醇，也可以是丙烯、丁烯、二甲醚，还可以是戊烷、己烷或HCFC-134a，HCFC-125等氟里昂及其代用品。

[0011]上述汽化器可以是一个，也可以连接多个汽化器。

[0012]本发明的液氨的汽化方法具有以下优点： [0013]1)采用二甲氧基甲烷、甲醇、乙醇等作为再沸器中的热媒介质，消除了液氨汽化时蒸汽凝水的液击现象及其形成条件； [0014]2)避免了空气中的水受冷结霜于氨气加热器换热管外表，避免换热热阻增加，充分利用换热效率； [0015]3)汽化器缩小了换热管内外温差，能保证设备的安全性，通过控制蒸汽压力波动，维持氨气连续稳定排出。

附图说明 [0016]图1是本发明液氨汽化工艺流程示意图。

[0017]附图中的标记分别表示： [0018]1、再沸器，包括：1〇、再沸器壳体，11、再沸器管束，12、蒸汽进口，13、蒸汽凝水出口，14、再沸器管箱，15、再沸器热媒蒸汽出口，16、再沸器热媒液进口； [0019]2、汽化器，包括：20、汽化器壳体，21、汽化器管束，22、汽化器管箱，23、液氨进口，24、氨蒸汽出口，25、汽化器热媒出口，26、汽化器热媒进口；31、蒸汽调节阀，32、氨调节阀，4、5、6、7、8、9均为管线。

[0020]以下结合附图和实施例对本发明作进一步详细说明。

具体实施方式 [0021]参见图1，按照本发明的技术方案，采用的设备包括再沸器和汽化器，再沸器1包括再沸器壳体10、再沸器管束11和再沸器管箱14。

汽化器2包括汽化器壳体20、汽化器管束21、汽化器管箱22。

再沸器1与汽化器2通过管线5、管线6相连接。

[0022]来自管线7的热蒸汽通过蒸汽调节阀31控制，再经过再沸器蒸汽进口12进入再沸器管束11;来自管线4和管线5的热媒液为二甲氧基甲烧，来自管线4的热媒液通过再沸器热媒液进口16进入再沸器1，再沸器管束11内的热蒸汽与热媒液二甲氧基甲烷换热后，蒸汽凝水通过蒸汽凝水出口13经管线8流出再沸器； [0023]热媒液二甲氧基甲烷在再沸器管束11汽化成二甲氧基甲烷过热气体，从再沸器热媒蒸汽出口15经过管线6,通过汽化器热媒进口26进入汽化器2,来自管线9的液氨经过液氨进口23进入汽化器管束21，汽化器2的热媒二甲氧基甲烷气体与管束内液氨换热后，汽化器2内冷凝的热媒液体再经过汽化器热媒出口25,进入管线5循环至再沸器1。

氨汽化器管束21内的液氨与汽化器的热媒气体换热后汽化成气态氨，气态氨经过汽化器氨蒸汽出口24进入管线19,通过调节阀门32直接控制氨气体流量和压力，并与蒸汽管线7上的蒸汽调节阀门31形成控制回路，保证连续稳定供应蒸汽并控制再沸器的换热量，维持氨气连续稳定排出。

[0024]下面是发明人给出的实施例，本发明不限于这些实施例。

[0025]实施例1: [0026]2.OMPa蒸汽以643kg/h通过蒸汽口进入再沸器管程，经换热管换热后加热再沸器内的二甲氧基甲烷，蒸汽凝结生成l〇6°C的水以643kg/h流出再沸器；将二甲氧基甲烷以536kg/h受热汽化，加热至温度为65°C，经换热后成为二甲氧基甲烷气体，并上升至汽化器内，二甲氧基甲烷气体加热汽化器管程，与汽化器管程内的氨换热后冷凝成热媒液，再流入再沸器内； [0027]来自外界的液氨以1360kg/h进入汽化器管程，接受热媒气体提供的热量后汽化成气态氨，温度52°C，压力1.OMPa，气态氨通过汽化器管程出口以1360kg/h流量排出，通过调节阀门直接控制氨气体流量和压力，并与蒸汽调节阀门形成控制回路，间接控制再沸器的换热量，维持氨气连续稳定排出。

[0028]实施例2: [0029]2.5MPa蒸汽以598kg/h通过蒸汽口进入再沸器管程，经换热管换热后加热再沸器内的二甲氧基甲烷，蒸汽凝结生成126°C的水以598kg/h流出再沸器；将二甲氧基甲烷以633kg/h受热汽化，加热至温度为121°C，经换热后成为二甲氧基甲烷气体，并上升至汽化器内，二甲氧基甲烷气体加热汽化器管程，与汽化器管程内的氨换热后冷凝成热媒液，再流入再沸器内，其中再沸器与汽化器相通； [0030]来自外界的液氨以1360kg/h进入汽化器管程，接受热媒气体提供的热量后汽化成气态氨，温度l〇5°C，压力2.0MPa，气态氨通过汽化器管程出口以1360kg/h流量排出，通过调节阀门直接控制氨气体流量和压力，并与蒸汽调节阀门形成控制回路，间接控制再沸器的换热量，维持氨气连续稳定排出。

[0031]当然，热媒介质还可以是甲醇、乙醇、二甲醚、丙烯、丁烯，戊烷、己烷或HCFC-134a，HCFC-125等氟里昂及其代用品，都能实现液氨的汽化。

Claims(2) 1.一种液氨的汽化方法，采用的设备包括相连通的再沸器和汽化器，其特征在于，按以下步骤操作：1)将加热蒸汽通过蒸汽口进入再沸器管程，经换热管换热后加热再沸器内的热媒，蒸汽冷凝生成的水流出再沸器，其中热媒为二甲氧基甲烷；2)热媒受热汽化，经换热后成为热媒气体，并上升至汽化器内，热媒气体加热汽化器管程，与汽化器管程内的氨换热后冷凝成热媒液，再流入再沸器内；3)来自外界的液氨进入汽化器管程，接受热媒气体提供的热量后汽化成气态氨，气态氨通过汽化器管程出口排出，通过调节阀门直接控制氨气体流量和压力，并与蒸汽调节阀门形成控制回路，间接控制再沸器的换热量，维持氨气连续稳定排出。

2.如权利要求1所述的方法，其特征在于，所述的汽化器是一个或多个。

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