CN201945138U - 合成氨驰放气中氩与甲烷的分离回收装置 - Google Patents

合成氨驰放气中氩与甲烷的分离回收装置 Download PDF

Info

Publication number
CN201945138U
CN201945138U CN201020544058XU CN201020544058U CN201945138U CN 201945138 U CN201945138 U CN 201945138U CN 201020544058X U CN201020544058X U CN 201020544058XU CN 201020544058 U CN201020544058 U CN 201020544058U CN 201945138 U CN201945138 U CN 201945138U
Authority
CN
China
Prior art keywords
pipeline
heat exchanger
main heat
evaporimeter
liquefier
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
CN201020544058XU
Other languages
English (en)
Inventor
刘景武
郑小平
马源
汤广斌
裴红珍
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
KAIFENG AIR SEPARATION GROUP CO Ltd
Original Assignee
KAIFENG AIR SEPARATION GROUP CO Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by KAIFENG AIR SEPARATION GROUP CO Ltd filed Critical KAIFENG AIR SEPARATION GROUP CO Ltd
Priority to CN201020544058XU priority Critical patent/CN201945138U/zh
Application granted granted Critical
Publication of CN201945138U publication Critical patent/CN201945138U/zh
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0233—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 characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0252—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 characterised by the separated product stream separation of hydrogen
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0257—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 characterised by the separated product stream separation of nitrogen
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/028—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 characterised by the separated product stream separation of noble gases
    • F25J3/0285—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 characterised by the separated product stream separation of noble gases of argon
    • 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/20—H2/N2 mixture, i.e. synthesis gas for or purge gas from ammonia synthesis
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

本实用新型涉及一种合成氨驰放气中氩与甲烷的分离回收装置，包括冷箱、原料驰放气管道、与原料驰放气管道相连通的设置有第一分子筛吸附器MS1和第二分子筛吸附器MS2的纯化***、提供分离液化所需冷量的制冷***、逐级分离原料驰放气的精馏***，所述的制冷***包括低压循环氮氩机TC1、中压循环氮压机TC2、低温增压透平膨胀机ET2、高温增压透平膨胀机ET1、主换热器E1、液化器E2，所述的精馏***包括闪蒸罐S1、安装有第一冷凝器K4和第一蒸发器K1的脱氢塔C1、安装有第二冷凝器K5和第二蒸发器K2的脱氮塔C2以及安装有第三冷凝器K6和第三蒸发器K3的产品塔C3，本实用新型产品的纯度高，回收率高。

Description

合成氨驰放气中氩与甲烷的分离回收装置
技术领域
本实用新型涉及一种气体分离领域，具体涉及一种合成氨驰放气中氩与甲烷的分离回收装置。
背景技术
合成氨生产工艺中所需的氮气来自空气，因此将随着空气带入氩气。而且由于原料中甲烷不能完全变换，或者在造气工艺中采用了甲烷化工序，而使合成原料气中增添了一些甲烷。由于氩和甲烷在合成***中是不起反应的，所以必然会在***中积累，因此合成***必须经常抽出一部分驰放气。在此驰放气中除了氩和甲烷以外，很自然地将包含一定数量的氢和氮。通常会将含量较高的氢和氮大部分回收利用，将剩余含氢、氮、氩、甲烷的驰放气去锅炉燃烧。
液体甲烷是一种优质能源，具有热值高、洁净、燃烧污染小等特点，且便于运输，是21世纪中国城市民用燃气首选燃料。液体甲烷可作为优质的车用燃料，与汽车烧汽油相比，它具有热值高、抗爆性好、燃烧完全、排气污染少、发动机寿命长、降低运输成本等优点，即使与使用压缩天然气的汽车相比，它也具有储存效率高、加一次气续行程远，车装钢瓶压力小、重量轻、数量小；建站不受供气管网的限制等优越之处。有利于环境保护，减少城市污染；液氩广泛应用于冶金、石化、机械、化肥、玻璃、军工、食品、医疗等领域。由于空气中氩的含量少(0.093％)，传统空分制氩，生产成本高。如果驰放气中的氩和甲烷不能得到回收利用将是极大的浪费。
发明内容
针对目前合成氨驰放气只回收氢、氮，而氩和甲烷不能得到分离提纯的不足，本实用新型提供一种制冷量利用率高、能耗低、产品纯度高的合成氨驰放气中氩与甲烷的分离回收装置。
本实用新型的技术方案是这样实现的：一种合成氨驰放气中氩与甲烷的分离回收装置，包括冷箱、原料驰放气管道、与原料驰放气管道相连通的设置有第一分子筛吸附器MS1和第二分子筛吸附器MS2的纯化***、提供分离液化所需冷量的制冷***、逐级分离原料驰放气的精馏***，所述的制冷***包括低压循环氮压机TC1、中压循环氮压机TC2、低温增压透平膨胀机ET2、高温增压透平膨胀机ET1、主换热器E1、液化器E2，外界的氮气通过管道与低压循环氮压机TC1相连通，低压循环氮压机TC1通过管道分别与低温增压透平膨胀机ET2、高温增压透平膨胀机ET1相连通，低温增压透平膨胀机ET2通过管道与液化器E2、主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接，高温增压透平膨胀机ET1通过管道与主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接；
所述的精馏***包括闪蒸罐S1、安装有第一冷凝器K4和第一蒸发器K1的脱氢塔C1、安装有第二冷凝器K5和第二蒸发器K2的脱氮塔C2以及安装有第三冷凝器K6和第三蒸发器K3的产品塔C3，外界的驰放气通过管道与纯化***相连通，纯化***通过穿过主换热器E1的管道与第三蒸发器K3相连接，第三蒸发器K3通过管道与液化器E2相连接，液化器E2通过管道与闪蒸罐S1相连接通，闪蒸罐S1通过管道与脱氢塔C1相连接，脱氢塔C1通过管道与脱氮塔C2相连接，脱氮塔C2通过管道与产品塔C3相连接；
外界的氮气通过管道与中压循环氮压机TC2相连接，中压循环氮压机TC2通过管道与主换热器E1相连接，主换热器E1通过管道与第二蒸发器K2相连接，第二蒸发器K2通过管道与第一蒸发器K1相连接，第一蒸发器K1又通过管道分别与脱氢塔C1中的第一冷凝器K4、脱氮塔C2中的第二冷凝器K5、产品塔C3中的第三冷凝器K6相连接，脱氢塔C1、脱氮塔C2、产品塔C3的上部分别通过管道与液化器E2相连接，液化器E2通过管道与主换热器E1相连接，主换热器E1通过管道与中压循环氮压机TC2相连接。
所述的闪蒸罐S1、主换热器E1、液化器E2、低温增压透平膨胀机ET2和高温增压透平膨胀机ET1的膨胀端均置于冷箱内。
所述的脱氮塔C2顶部通过穿过液化器E2、主换热器E1的管道与电加热器HE相连接，电加热器HE通过管道与纯化***相连接。
所述的低压循环氮压机TC1通过管道与高温透平膨胀机增压端B1相连接，高温透平膨胀机增压端B1通过管道与第一水冷却器WE1相连接，第一水冷却器WE1通过管道与高温透平膨胀机ET1相连接；所述的低压循环氮压机TC1通过管道与低温透平膨胀机增压端B2相连接，低温透平膨胀机增压端B2通过管道与第二水冷却器WE2相连接，第二水冷却器WE2穿过主换热器E1与低温透平膨胀机ET2相连接。
本实用新型具有如下的积极效果：本实用新型通过双膨胀制冷，减少有效能损失，降低装置能耗；通过设置三个精馏塔，使产品的纯度高，且回收率高。
附图说明
图1为本实用新型的结构示意图。
具体实施方式
如图1所示，一种合成氨驰放气中氩与甲烷的分离回收装置，包括冷箱、原料驰放气管道1、与原料驰放气管道1相连通的设置有第一分子筛吸附器MS1和第二分子筛吸附器MS2的纯化***、提供分离液化所需冷量的制冷***、逐级分离原料驰放气的精馏***，所述的制冷***包括低压循环氮压机TC1、中压循环氮压机TC2、低温增压透平膨胀机ET2、高温增压透平膨胀机ET1、主换热器E1、液化器E2，外界的氮气通过管道与低压循环氮压机TC1相连通，低压循环氮压机TC1通过管道分别与低温增压透平膨胀机ET2、高温增压透平膨胀机ET1相连通，低温增压透平膨胀机ET2通过管道与液化器E2、主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接，高温增压透平膨胀机ET1相连通通过管道与主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接；
所述的精馏***包括闪蒸罐S1、安装有第一冷凝器K4和第一蒸发器K1的脱氢塔C1、安装有第二冷凝器K5和第二蒸发器K2的脱氮塔C2以及安装有第三冷凝器K6和第三蒸发器K3的产品塔C3，外界的驰放气通过管道与纯化***相连通，纯化***通过穿过主换热器E1的管道与第三蒸发器K3相连接，第三蒸发器K3通过管道与液化器E2相连接，液化器E2通过管道与闪蒸罐S1相连接通，闪蒸罐S1通过管道与脱氢塔C1相连接，脱氢塔C1通过管道与脱氮塔C2相连接，脱氮塔C2通过管道与产品塔C3相连接；
外界的氮气通过管道与中压循环氮压机TC2相连接，中压循环氮压机TC2通过管道与主换热器E1相连接，主换热器E1通过管道与第二蒸发器K2相连接，第二蒸发器K2通过管道与第一蒸发器K1相连接，第一蒸发器K1又通过管道分别与脱氢塔C1中的第一冷凝器K4、脱氮塔C2中的第二冷凝器K5、产品塔C3中的第三冷凝器K6，脱氢塔C1、脱氮塔C2、产品塔C3的上部分别通过管道与液化器E2相连接，液化器E2通过管道与中压循环氮压机TC2相连接。
所述的闪蒸罐S1、主换热器E1、液化器E2、低温增压透平膨胀机ET2和高温增压透平膨胀机ET1的膨胀端均置于冷箱内。所述的脱氮塔C2顶部通过穿过液化器E2、主换热器E1的管道与电加热器HE相连接，电加热器HE通过管道与纯化***相连接。所述的低压循环氮压机TC1通过管道与高温透平膨胀机增压端B1相连接，高温透平膨胀机增压端B1通过管道与第一水冷却器WE1相连接，第一水冷却器WE1通过管道与高温透平膨胀机ET1相连接；所述的低压循环氮压机TC1通过管道与低温透平膨胀机增压端B2相连接，低温透平膨胀机增压端B2通过管道与第二水冷却器WE2相连接，第二水冷却器WE2穿过主换热器E1与低温透平膨胀机ET2相连接。
一种分离氩与甲烷的方法，其方法如下：
1)压力为0.5Mpa-10.0Mpa原料驰放气通过原料驰放气管道1进入纯化***中第一分子筛吸附器MS1或第二分子筛吸附器MS2，除去驰放气中微量的水份、二氧化碳、氨等杂质，净化后的驰放气通过净化后驰放气管道2去主换热器E1换热，被冷却到气液混合状态，然后出主换热器E1通过第一气液混合管道3去产品塔C3中的第三蒸发器K3，将液态甲烷蒸发的同时自身得到再次冷却，冷却后通过第二气液混合管道4去液化器E2继续冷却并液化，液化后通过第一液体管道5进闪蒸罐S1节流闪蒸；
2)所述1)中的闪蒸罐S1将大部分的氢闪蒸分离，含氢较多的富氢通过富氢管道6经主换热器E1复热后通过富氢排除管道7出冷箱，闪蒸罐底部的液体通过第二液体管道8进入脱氢塔C1，在脱氢塔C1进行热质交换、冷凝蒸发，在脱氢塔C1顶部得到废氢气，在脱氢塔C1底部得到贫氢液；
3)所述2)中的脱氢塔C1顶部得到废氢气通过废氢气管道16经液化器E2、主换热器E1复热后通过废氢气排出管道17出冷箱，脱氢塔C1底部得到贫氢液通过贫氢液管道9送入脱氮塔C2，在脱氮塔C2中进行热质交换、冷凝蒸发，在脱氮塔C2顶部得到氮气，在脱氮塔C2底部得到贫氮液；
4)所述3)中脱氮塔C2顶部得到氮气通过第一氮气管道14经液化器E2、主换热器E1复热出冷箱，通过第二氮气管道15在电加热器HE中加热至170～180℃，去第二分子筛吸附器MS2或第一分子筛吸附器MS1再生活化分子筛，然后通过消音器SL放空；脱氮塔C2底部得到贫氮液通过贫氮液管道10送入产品塔C3，在产品塔C3中进行热质交换、冷凝蒸发，在产品塔C3顶部得到废氩气通过废氩气管道13出冷箱，在产品塔C3上部得到纯度为99.999％以上的液氩通过液氩管道12出冷箱，在产品塔C3底部得到纯度为99％以上的液体甲烷通过液化天然气管道11出冷箱；
5)低压循环氮压机TC1通过第十氮气管道18将来自外界的氮气压缩至0.4Mpa-1.0Mpa，分成两部分，一部分氮气通过第三氮气管道21去高温透平膨胀机ET1的增压端B1增压并经第一水冷却器WE1冷却后，通过第一水冷却管道22去高温透平膨胀机ET1膨胀，膨胀后通过第一膨胀机管道23去主换热器E1提供高温冷量，复热后通过第一循环管道24出冷箱，去低压循环氮压机TC1循环压缩；另一部分氮气通过第四氮气管道25去低温透平膨胀机ET2的增压端B2增压并经第二水冷却器WE2冷却后，通过第二水冷却管道26去主换热器E1进一步降温后抽出，通过第一主换热器管道27去低温透平膨胀机ET2膨胀，膨胀后通过第二膨胀机管道28去液化器E2、主换热器E1，提供低温冷量，复热后通过第二循环管道29出冷箱，去低压循环氮压机TC1循环压缩。
6)中压循环氮压机TC2通过第十一氮气管道19将来自外界的氮气压缩至1.5Mpa-2.5Mpa，通过第五氮气管道31在主换热器E1中冷却后抽出，通过第一液氮管道32去脱氮塔C2作为第二蒸发器K2的热源，将贫氮液蒸发，蒸发贫氮液的同时再次冷却，冷却后通过第二液氮管道33去脱氢塔C1作为第一蒸发器K1的热源，将贫氢液蒸发后冷却液化为液氮，液氮通过第六液氮管道34分成三部分，节流后分别通过第三液氮管道35、第四液氮管道37、第五液氮管道39去脱氢塔C1、脱氮塔C2、产品塔C3中为第一冷凝器K4、第二冷凝器K5、第三冷凝器K6提供冷量，脱氢塔C1、脱氮塔C2、产品塔C3的冷凝器中汽化后的氮气通过第六氮气管道36、第七氮气管道38、第八氮气管道40合并后第九氮气管道41去液化器E2、主换热器E1，复热后出冷箱，通过第十一氮气管道30去中压循环氮压机TC2循环压缩。
本实用新型通过双膨胀制冷，减少有效能损失，降低装置能耗，较单膨胀制冷能耗降低5％左右。通过设置三个精馏塔，使产品的纯度高，回收率高。液氩纯度达99.999％，回收率达96％；液体甲烷的纯度99％以上，回收率99％以上。
本实用新型并不局限于上述的具体实施方式，上述的具体实施方式仅仅是示意性的，并不是限制性的，本领域的普通技术人员在本实用新型的启示下，在不脱离本实用新型宗旨和权利要求所保护的范围情况下，还可以作出很多形式，这些均属于本实用新型的保护范围之内。

Claims (4)

1.一种合成氨驰放气中氩与甲烷的分离回收装置，包括冷箱、原料驰放气管道(1)、与原料驰放气管道(1)相连通的设置有第一分子筛吸附器MS1和第二分子筛吸附器MS2的纯化***、提供分离液化所需冷量的制冷***、逐级分离原料驰放气的精馏***，其特征在于：
所述的制冷***包括低压循环氮压机TC1、中压循环氮压机TC2、低温增压透平膨胀机ET2、高温增压透平膨胀机ET1、主换热器E1、液化器E2，外界的氮气通过管道与低压循环氮压机TC1相连通，低压循环氮压机TC1通过管道分别与低温增压透平膨胀机ET2、高温增压透平膨胀机ET1相连通，低温增压透平膨胀机ET2通过管道与液化器E2、主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接，高温增压透平膨胀机ET1通过管道与主换热器E1相连接，主换热器E1通过管道与低压循环氮压机TC1相连接；
所述的精馏***包括闪蒸罐S1、安装有第一冷凝器K4和第一蒸发器K1的脱氢塔C1、安装有第二冷凝器K5和第二蒸发器K2的脱氮塔C2以及安装有第三冷凝器K6和第三蒸发器K3的产品塔C3，外界的驰放气通过管道与纯化***相连通，纯化***通过穿过主换热器E1的管道与第三蒸发器K3相连接，第三蒸发器K3通过管道与液化器E2相连接，液化器E2通过管道与闪蒸罐S1相连接通，闪蒸罐S1通过管道与脱氢塔C1相连接，脱氢塔C1通过管道与脱氮塔C2相连接，脱氮塔C2通过管道与产品塔C3相连接；
外界的氮气通过管道与中压循环氮压机TC2相连接，中压循环氮压机TC2通过管道与主换热器E1相连接，主换热器E1通过管道与第二蒸发器K2相连接，第二蒸发器K2通过管道与第一蒸发器K1相连接，第一蒸发器K1又通过管道分别与脱氢塔C1中的第一冷凝器K4、脱氮塔C2中的第二冷凝器K5、产品塔C3中的第三冷凝器K6相连接，脱氢塔C1、脱氮塔C2、产品塔C3的上部分别通过管道与液化器E2相连接，液化器E2通过管道与主换热器E1相连接，主换热器E1通过管道与中压循环氮压机TC2相连接。
2.根据权利要求1所述的合成氨驰放气中氩与甲烷的分离回收装置，其特征在于：所述的闪蒸罐S1、主换热器E1、液化器E2、低温增压透平膨胀机ET2和高温增压透平膨胀机ET1的膨胀端均置于冷箱内。
3.根据权利要求1所述的合成氨驰放气中氩与甲烷的分离回收装置，其特征在于：所述的脱氮塔C2顶部通过穿过液化器E2、主换热器E1的管道与电加热器HE相连接，电加热器HE通过管道与纯化***相连接。
4.根据权利要求1所述的合成氨驰放气中氩与甲烷的分离回收装置，其特征在于：所述的低压循环氮压机TC1通过管道与高温透平膨胀机增压端B1相连接，高温透平膨胀机增压端B1通过管道与第一水冷却器WE1相连接，第一水冷却器WE1通过管道与高温透平膨胀机ET1相连接；所述的低压循环氮压机TC1通过管道与低温透平膨胀机增压端B2相连接，低温透平膨胀机增压端B2通过管道与第二水冷却器WE2相连接，第二水冷却器WE2穿过主换热器E1与低温透平膨胀机ET2相连接。
CN201020544058XU 2010-09-27 2010-09-27 合成氨驰放气中氩与甲烷的分离回收装置 Expired - Fee Related CN201945138U (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201020544058XU CN201945138U (zh) 2010-09-27 2010-09-27 合成氨驰放气中氩与甲烷的分离回收装置

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201020544058XU CN201945138U (zh) 2010-09-27 2010-09-27 合成氨驰放气中氩与甲烷的分离回收装置

Publications (1)

Publication Number Publication Date
CN201945138U true CN201945138U (zh) 2011-08-24

Family

ID=44472478

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201020544058XU Expired - Fee Related CN201945138U (zh) 2010-09-27 2010-09-27 合成氨驰放气中氩与甲烷的分离回收装置

Country Status (1)

Country Link
CN (1) CN201945138U (zh)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101968298A (zh) * 2010-09-27 2011-02-09 开封空分集团有限公司 合成氨驰放气中氩与甲烷的分离回收装置及方法
CN102500194A (zh) * 2011-09-30 2012-06-20 张世田 化工尾气分离回收工艺及装置
CN103925773A (zh) * 2013-11-05 2014-07-16 北京蓝图工程设计有限公司 一种合成氨尾气制备液化天然气及氮氢气的方法
CN104154705A (zh) * 2014-08-15 2014-11-19 苏州市兴鲁空分设备科技发展有限公司 一种合成氨废气分离装置
CN104390427A (zh) * 2014-10-21 2015-03-04 杭州福斯达实业集团有限公司 高低温双膨胀节能型制氮装置及制氮方法
CN114891546A (zh) * 2022-06-08 2022-08-12 佛燃能源集团股份有限公司 利用合成氨驰放气制取氢气和燃料级天然气的***及方法

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101968298A (zh) * 2010-09-27 2011-02-09 开封空分集团有限公司 合成氨驰放气中氩与甲烷的分离回收装置及方法
CN101968298B (zh) * 2010-09-27 2013-10-02 开封空分集团有限公司 合成氨驰放气中氩与甲烷的分离回收装置及方法
CN102500194A (zh) * 2011-09-30 2012-06-20 张世田 化工尾气分离回收工艺及装置
CN103925773A (zh) * 2013-11-05 2014-07-16 北京蓝图工程设计有限公司 一种合成氨尾气制备液化天然气及氮氢气的方法
CN103925773B (zh) * 2013-11-05 2016-08-17 北京蓝图工程设计有限公司 一种合成氨尾气制备液化天然气及氮氢气的方法
CN104154705A (zh) * 2014-08-15 2014-11-19 苏州市兴鲁空分设备科技发展有限公司 一种合成氨废气分离装置
CN104390427A (zh) * 2014-10-21 2015-03-04 杭州福斯达实业集团有限公司 高低温双膨胀节能型制氮装置及制氮方法
CN104390427B (zh) * 2014-10-21 2017-01-18 杭州福斯达深冷装备股份有限公司 高低温双膨胀节能型制氮装置及制氮方法
CN114891546A (zh) * 2022-06-08 2022-08-12 佛燃能源集团股份有限公司 利用合成氨驰放气制取氢气和燃料级天然气的***及方法
CN114891546B (zh) * 2022-06-08 2022-12-09 佛燃能源集团股份有限公司 利用合成氨驰放气制取氢气和燃料级天然气的***及方法

Similar Documents

Publication Publication Date Title
CN101968298B (zh) 合成氨驰放气中氩与甲烷的分离回收装置及方法
CN102419071B (zh) 合成氨驰放气中甲烷和氩气的分离回收装置及回收方法
CN102115684B (zh) 一种由焦炉煤气生产液化天然气的方法
CN201945138U (zh) 合成氨驰放气中氩与甲烷的分离回收装置
CN101033910B (zh) 集成空气分离与液化天然气冷量回收***
CN101280235A (zh) 一种以焦炉煤气为原料生产液化天然气的方法
CN102538398B (zh) 一种含氮氧煤矿瓦斯提纯分离液化工艺及提纯分离液化***
WO2021043182A1 (zh) 一种利用lng冷能的空分装置和方法
CN103215093B (zh) 小型撬装式氮膨胀天然气液化***及其方法
CN105783424B (zh) 利用液化天然气冷能生产高压富氧气体的空气分离方法
CN103363778B (zh) 小型撬装式单阶混合制冷剂天然气液化***及其方法
CN108795508B (zh) 一种利用氮气和氦气膨胀制冷分离焦炉煤气的方法
CN102732349A (zh) 一种生产液化天然气的方法
CN101747131B (zh) 利用膜分离与低温精馏从焦炉煤气中提取氢和甲烷的方法
CN105180595A (zh) 一种制取富氢气和液态甲烷的***及方法
CN104804788A (zh) 用垃圾热解气制取lng的方法和***
CN102435045A (zh) 液氮洗涤净化合成气及其深冷分离回收lng装置
CN202382516U (zh) 合成氨驰放气中甲烷和氩气的分离回收装置
CN202382518U (zh) 液氮洗涤净化合成气及其深冷分离回收lng装置
CN201377962Y (zh) 从含甲烷混合气中制取压缩天然气的设备
CN217661593U (zh) 低温精馏提纯回收二氧化碳装置
CN105157348B (zh) 一种回收lng的液氮洗装置及其方法
CN202630585U (zh) 一种空气分离设备
CN205079542U (zh) 一种制取富氢气和液态甲烷的***
CN107024074B (zh) 一种氮气单级膨胀制冷回收甲醇合成尾气中甲烷制备lng的装置及其方法

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20110824

Termination date: 20140927

EXPY Termination of patent right or utility model