CN110173961B - 一种基于高效板翅式换热器的氢气和轻烃深冷分离装置 - Google Patents
一种基于高效板翅式换热器的氢气和轻烃深冷分离装置 Download PDFInfo
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Abstract
本发明公开了基于高效板翅式换热器的氢气和轻烃深冷分离装置及方法,包括深冷分离冷箱(Ⅰ)、膨胀单元(Ⅱ)和泵加压单元(Ⅲ)。深冷分离冷箱包括用于换热的三个板翅式换热器(E1、E2、E3)、用于分离富氢气和液体轻烃的第一分离罐(D1)及连接管道、用于分离富氢气和液体轻烃的第二分离器(D2)及连接管道、用于收集液体产品的液体产品收集罐(D3)。膨胀单元包括用于高压富氢气膨胀的第一膨胀机(K1)、用于低压富氢气膨胀的第二膨胀机(K2)。本发明能够实现轻烃回收率达到99.96%,富氢气产品中的总烯烃含量小于1000ppm,氢气含量大于94%,装置占地少,能耗低,适用于分离低碳烷烃脱氢产物的深冷分离装置。
Description
技术领域
本发明涉及一种基于高效板翅式换热器的氢气和轻烃深冷分离装置及方法,属于石化低温气体分离领域。
背景技术
丙烯是重要的化工原料,可用于生产聚丙烯、丙烯酸、环氧丙烷等。传统丙烯来源是蒸汽热裂解装置和催化裂化装置,随着丙烷脱氢、甲醇制烯烃生产丙烯等新工艺技术的开发成熟,近年来采用相应技术的装置数量逐年增加,而丙烷催化脱氢制丙烯的装置由于流程短、投资成本低、原料成本低等特点,受到很多投资者的青睐。
国内的丙烷装置脱氢反应产物中包含乙烯等副产物,需要冷箱分离装置达到更低的分离温度;同时目前的冷箱分离装置中的膨胀机除承担膨胀机制冷的作用外,还需承担冷凝分离烃类的功能,这就使膨胀机有可能处于高转速、带液的的状态下工作,严重影响膨胀机的寿命。
发明内容
本发明的目的在于:提供一种基于高效板翅式换热器的氢气和轻烃深冷分离装置及方法,在进料高乙烯含量的条件下,能使干气产品和循环氢气中乙烯含量达到1000ppm以下;同时,膨胀机不需要承担冷凝分离烃类的功能,处于完全无液的状态下运行,保证了膨胀机的安全;在不需要膨胀机冷凝分离,使用针对气液两相高密度差工况的高效板翅式换热器,保证第一换热器和第二换热器的冷凝分离效果满足装置整体要求。
为实现上述目的,本发明可采取下述技术方案:一种基于高效板翅式换热器的氢气和轻烃深冷分离装置,它包括深冷分离冷箱,膨胀单元,泵加压单元三部分组成,所述深冷分离冷箱入口与管道连通,并经过第一换热器后与第一分离器相连,所述第一换热器与第一分离器相连,并第一分离器底部分离出的液相物流经节流阀和液体产品收集罐的入口管道连通;所述第一分离器顶部分离出的气相物流通过管道,依次与第二换热器、第二分离器连通。
作为优选:所述第二分离器底部分离出的液相物流经节流阀和液体产品收集罐的入口管道连通;所述第二分离器顶部分离出的气相物流通过管道与第二换热器连接,所述第二分离器顶部出来的气相物流在第二换热器中复热后通过管道与第一膨胀机连通;所述第一膨胀机出来的物流分成两股,一股通过管道与第二换热器连通,再通过管道分别经第一换热器、第三换热器后汇集于管道,作为富氢气产品送出本装置;所述另一股通过管道与第二换热器连通,在第二换热器稍微复热后通过管道、第二膨胀机后与第二换热器连通,作为循环氢气。
作为优选:所述第三换热器连接含丙烷的原料工艺物流,并且第三换热器的入口与管道连通,所述原料工艺物流经换热后分成两股,一股连接管道、第二换热器、节流阀后,返回第二换热器与管道来的循环氢气混合,经第二换热器、管道与第一换热器连通;所述另一股通过节流阀、管道与第一换热器连通,在第一换热器中与管道来的物流混合,作为联合进料产品,通过管道送出本装置。
作为优选:所述的液体产品收集罐的顶部气相为闪蒸汽产品,通过管道、第三换热器后送出本装置;所述底部分离出的液相为液体产品),并通过管道、液体产品泵、第三换热器加压复热后送出本装置。
作为优选:所述的第一换热器、第二换热器、第三换热器均为适用于气液两相高密度差工况的高效板翅式换热器。
作为优选:所述的第一膨胀机、第二膨胀机均为采用发电机制动的透平膨胀机。
作为优选:所述的液体产品泵为采用电机驱动的立式离心筒袋泵。
作为优选:所述的第一分离器、第二分离器、液体产品收集罐均为采用高效丝网除雾器的重力分离器。
本发明的积极效果是:上述方案深冷分离装置设置第一换热器和第二换热器两级冷却,在第一换热器中将大部分碳三组分冷凝下来后,将液相分离出来,避免液相的进一步冷却而消耗冷量;第二换热器将工艺气冷却至足够低的温度后,使剩余的碳二组分能够冷凝分离出来,使第二分离器气相组分就能达到干气产品和循环氢气的纯度要求,其中氢气纯度达到94%以上,总烯烃含量小于1000ppm,装置的碳三烃类回收率达到99.96%。
本发明进一步的积极效果是:上述技术方案进膨胀机物料都为经换热器复热后的过热状态,膨胀机入口和出口都不带液,在30000转/分钟以上的高速运转下能够安全、长期稳定运行。
本发明进一步的积极效果是:上述技术方案采用工艺气自身压力膨胀制冷和原料丙烷的气化潜热给装置提供冷量,无需外部制冷循环系统提供冷量,而且膨胀机可驱动发电机输出电能,只有液体产品泵需电机驱动,装置整体能耗低,运行成本低,具有很好的经济性。
附图说明
图1是本发明的连接结构示意图。
具体实施方式
如图1所示,本发明用于分离含有氢气和甲烷、乙烯、乙烷、丙烯、丙烷等轻烃的脱氢反应产物工艺气体(进料1),包括深冷分离冷箱Ⅰ,膨胀单元Ⅱ,泵加压单元Ⅲ。深冷分离冷箱包含第一换热器E1、第二换热器E2、第三换热器E3、第一分离器D1、第二分离器D2、液体产品收集罐D3。含有氢气20~60%、甲烷2~5%、乙烯0.1~0.7%、乙烷1~3%、丙烯10~30%、丙烷20~50%等轻烃的脱氢反应产物工艺气体进料1,压力1.0~2.0MPaG,与深冷分离冷箱Ⅰ入口管道1连通,经过第一换热器E1冷却、冷凝至-30℃~-60℃后通过管道2与第一分离器D1入口连通,进行气液分离,从第一分离器D1底部分离出的液相物流经节流阀V1节流至0.2~1.0MpaG后,和液体产品收集罐D3的入口管道27连通;从第一分离器D1顶部分离出的气相物流通过管道3,4,依次与第二换热器E2、第二分离器D2连通。
经第二换热器E2进一步冷凝至-100℃~-130℃后,通过管道4与第二分离器D2入口连通,进行气液分离,从第二分离器D2底部分离出的液相物流经节流阀V2节流至0.2~1.0MpaG后,和液体产品收集罐D3的入口管道27连通;从第二分离器D2顶部分离出的气相物流通过管道5与第二换热器E2连接,在第二换热器E2中稍微复热5℃~10℃后通过管道6与第一膨胀机K1连通,膨胀至压力0.6~0.8MpaG,温度-105℃~-140℃,同时驱动发电机发电回收膨胀功。从第一膨胀机K1出来的物流分成两股,一股通过管道8与第二换热器E2连通,经第二换热器E2复热至-35℃~-65℃,再通过管道17,18,19,20分别经第一换热器E1、第三换热器E3复热至常温后汇集于管道21,作为富氢气产品(产品4)送出本装置;另一股通过管道9与第二换热器E2连通,在第二换热器E2稍微复热5℃~10℃后通过管道10与第二膨胀机K2连通,膨胀至压力0.2~0.5MpaG,温度-110℃~-140℃,同时驱动发电机发电回收膨胀功。从第二膨胀机K2出来的物流通过管道11与第二换热器E2连通,作为循环氢气。
主要含丙烷的原料工艺物流进料2,压力1.7~2.5MPaG与第三换热器E3入口管道22连通,经第三换热器E3冷却至-25℃~-60℃后分成两股,一股通过管道25,26、第二换热器E2继续冷却以及节流阀V4后,返回第二换热器E2与管道11来的循环氢气进行气液混合,在第二换热器E2中吸收热物流的热量而使气液混合物蒸发,达到提供冷量的目的,蒸发完后的气相通过管道13与第一换热器E1连通;另一股通过节流阀V3、管道13与第一换热器E1连通,在第一换热器E1中与管道13来的物流进行气液混合,在第一换热器E1中吸收热物流的热量而使气液混合物蒸发,达到进一步提供冷量的目的,蒸发完并被加热至常温后的气相作为联合进料产品(产品1),通过管道15送出本装置。
液体产品收集罐D3顶部少量气相为闪蒸汽产品(产品3),通过管道31,32、第三换热器E3复热至常温后送出本装置;底部液相为液体产品(产品2),通过管道28,29,30、液体产品泵P1加压至3.0~5.0MPaG、第三换热器E3复热至常温后送出本装置。
上述实施例是本发明的具体实施方式。对于分离含有氢气和甲烷、乙烯、乙烷、丙烯、丙烷等轻烃的脱氢反应产物工艺气体的深冷分离装置可以做出多种等同的组合或变化,均属于本发明的保护范围。
Claims (6)
1.一种基于高效板翅式换热器的氢气和轻烃深冷分离装置,它包括深冷分离冷箱(Ⅰ),膨胀单元(Ⅱ),泵加压单元(Ⅲ)三部分组成,其特征在于所述深冷分离冷箱(Ⅰ)入口与管道(1)连通,并经过第一换热器(E1)后与第一分离器(D1)相连,所述第一分离器(D1)底部分离出的液相物流经节流阀(V1)和液体产品收集罐(D3)的入口管道(27)连通;所述第一分离器(D1)顶部分离出的气相物流通过管道(3,4),依次与第二换热器(E2)、第二分离器(D2)连通;
所述第二分离器(D2)底部分离出的液相物流经节流阀(V2)和液体产品收集罐(D3)的入口管道(27)连通;所述第二分离器(D2)顶部分离出的气相物流通过管道(5)与第二换热器(E2)连接,所述第二分离器(D2)顶部出来的气相物流在第二换热器(E2)中复热后通过管道(6)与第一膨胀机(K1)连通;所述第一膨胀机(K1)出来的物流分成两股,一股通过管道(8)与第二换热器(E2)连通,再通过管道(17,18,19,20)分别经第一换热器(E1)、第三换热器(E3)后汇集于管道(21),作为富氢气产品(产品4)送出本装置;所述另一股通过管道(9)与第二换热器(E2)连通,在第二换热器(E2)稍微复热后通过管道(10,11)、第二膨胀机(K2)后与第二换热器(E2)连通,作为循环氢气;
所述第三换热器(E3)连接含丙烷的原料工艺物流(进料2),并且第三换热器(E3)的入口与管道(22)连通,所述原料工艺物流(进料2)经换热后分成两股,一股连接管道(25,26)、第二换热器(E2)、节流阀(V4)后,返回第二换热器(E2)与管道(11)来的循环氢气混合,经第二换热器(E2)、管道(13)与第一换热器(E1)连通;所述另一股通过节流阀(V3)、管道(13)与第一换热器(E1)连通,在第一换热器(E1)中与管道(13)来的物流混合,作为联合进料产品(产品1),通过管道(15)送出本装置。
2.根据权利要求1所述基于高效板翅式换热器的氢气和轻烃深冷分离装置,其特征在于所述的液体产品收集罐(D3)的顶部气相为闪蒸汽产品(产品3),通过管道(31,32)、第三换热器(E3)后送出本装置;所述底部分离出的液相为液体产品(产品2),并通过管道(28,29,30)、液体产品泵(P1)、第三换热器(E3)加压复热后送出本装置。
3.根据权利要求1所述基于高效板翅式换热器的氢气和轻烃深冷分离装置,其特征在于所述的第一换热器(E1)、第二换热器(E2)、第三换热器(E3)均为适用于气液两相高密度差工况的高效板翅式换热器。
4.根据权利要求1所述基于高效板翅式换热器的氢气和轻烃深冷分离装置,其特征在于所述的第一膨胀机(K1)、第二膨胀机(K2)均为采用发电机制动的透平膨胀机。
5.根据权利要求2所述基于高效板翅式换热器的氢气和轻烃深冷分离装置,其特征在于所述的液体产品泵(P1)为采用电机驱动的立式离心筒袋泵。
6.根据权利要求1所述基于高效板翅式换热器的氢气和轻烃深冷分离装置,其特征在于所述的第一分离器(D1)、第二分离器(D2)、液体产品收集罐(D3)均为采用高效丝网除雾器的重力分离器。
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