CN203837409U - 从富甲烷气中制取液化天然气和富氢产品的装置 - Google Patents

从富甲烷气中制取液化天然气和富氢产品的装置 Download PDF

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CN203837409U
CN203837409U CN201320852728.8U CN201320852728U CN203837409U CN 203837409 U CN203837409 U CN 203837409U CN 201320852728 U CN201320852728 U CN 201320852728U CN 203837409 U CN203837409 U CN 203837409U
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侯智德
丁友胜
蒋旭
施晓俊
王第珲
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ZOKO ENERGY EQUIPMENT CO Ltd
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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
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    • 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
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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
    • F25J3/0228—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
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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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/14—Coke-ovens gas
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
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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
    • 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
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    • 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
    • F25J2270/18—External refrigeration with incorporated cascade 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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Abstract

本实用新型涉及一种从富甲烷气中制取液化天然气和富氢产品的装置。装置包括混合冷剂压缩机制冷系统、预冷系统、液化冷箱系统、氮气压缩机系统；方法包括混合冷剂循环过程、富甲烷气液化及分离过程、氮气冷剂循环过程。本实用新型精馏塔产生的低温富氢气体、富氮气体和冷凝器外部液氮蒸发的低温氮气用于过冷进冷凝蒸发器前的液氮，不同于传统的过冷液化天然气，整个换热器过程的冷流体和热流体的换热曲线更匹配，且换热器冷端温差更小，因此换热效率更高、能耗更低。

Description

从富甲烷气中制取液化天然气和富氢产品的装置
技术领域
本实用新型涉及一种从富甲烷气中制取液化天然气和富氢产品的装置。
背景技术
制取富甲烷气较为常见的是焦炉煤气通过甲烷化反应来提高热值，使绝大部分一氧化碳、二氧化碳转化成甲烷，所得的合成气再经水洗涤脱油洗萘、脱硫后的净化后得到的甲烷体积分数为40～50%以上，另富含氢气和氮气。富甲烷气再经低温液化、低温精馏制备出LNG和富氢产品。富甲烷化的焦炉煤气经过净化、液化分离制备出液化天然气不仅可缓解国内天然气短缺的问题，而且可以促进焦化与能源行业的技术进步与产业发展，发展焦炉煤气制LNG项目可产生明显的经济效益、环境效益与社会效益，对焦炉煤气回收利用产业具有重要意义。
富甲烷气与常规天然气组成有较大的区别，氮气、氢气含量相对较高，因此液化和分离工艺更复杂、单位产品能耗更高。
传统的混合制冷联合液氮制冷从富甲烷气中制取液化天然气和富氢产品的工艺，精馏塔产生的低温富氢气、富氮气和冷凝器产生的低温氮气以两种方式提供冷量：一种是返回主换热器为所有热流股提供冷量，一种是用于过冷精馏塔底馏出的液化天然气。
申请号为201210065876.5、名称为从富甲烷气中脱氢氮并生产液化天然气的工艺和装置的中国专利，申请号为201110291609.5、名称为从富甲烷气中脱氢气、氮气、一氧化碳并生产液化天然气的工艺的中国专利，这些现有技术在制冷效果、富甲烷气液化及分离效果等方面仍存在不足，单位能耗较高，而且对富氢气体制取不足，易造成浪费。
实用新型内容
本实用新型的目的在于克服现有技术中存在的上述不足，而提供一种设计合理、节能、成本低的从富甲烷气中制取液化天然气和富氢产品的装置。
本实用新型解决上述问题所采用的技术方案是：一种从富甲烷气中制取液化天然气和富氢产品的装置，包括混合冷剂压缩机制冷系统、预冷系统、液化冷箱系统、氮气压缩机系统；所述的混合冷剂压缩机制冷系统包括混合冷剂压缩机、一号中间冷却器、一号末级冷却器、中间气液分离罐；混合冷剂压缩机具有压缩一段和压缩二段；所述的预冷系统包括预冷换热器、冷剂气液分离器；所述的液化冷箱系统包括冷却换热器、液化换热器、液氮过冷换热器、脱氮精馏塔、脱氢精馏塔；脱氢精馏塔的塔顶设有一号塔顶冷凝蒸发器和一号塔顶气液分离器；脱氮精馏塔的塔底设有塔底再沸器，塔顶设有二号塔顶冷凝蒸发器和二号塔顶气液分离器；所述的氮气压缩机制冷系统包括氮气压缩机、二号中间冷却器、二号末级冷却器；
混合冷剂压缩机的压缩一段、一号中间冷却器、中间气液分离罐、混合冷剂压缩机的压缩二段、一号末级冷却器、预冷换热器的热流体段、冷剂气液分离器的混合料进口依次接通；冷剂气液分离器的气体出口、冷却换热器的热流体段、液化换热器的热流体段、塔底再沸器、液化换热器的热流体段、液化换热器的冷流体段、冷却换热器的冷流体段依次接通；冷剂气液分离器的液体出口、冷却换热器的热流体段、冷却换热器的冷流体段依次接通；冷却换热器的冷流体段与混合冷剂压缩机的压缩一段接通；这部分结构构成了混合冷剂的循环线路；
预冷换热器的热流体段、冷却换热器的热流体段、液化换热器的热流体段、脱氢精馏塔进料口依次接通；脱氢精馏塔的塔顶气体出口、一号塔顶冷凝蒸发器的冷凝段、一号塔顶气液分离器进料口依次接通；一号塔顶气液分离器的液体出口与脱氢精馏塔的回流液入口接通，一号塔顶气液分离器的气体出口、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、预冷换热器的冷流体段依次接通；脱氢精馏塔的塔底液体出口与脱氮精馏塔的进料口接通；脱氮精馏塔的塔顶气体出口、二号塔顶冷凝蒸发器的冷凝段、二号塔顶气液分离器的进料口依次接通；二号塔顶气液分离器的液体出口与脱氮精馏塔的回流液入口接通，二号塔顶气液分离器的气体出口、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、预冷换热器的冷流体段依次接通；脱氮精馏塔的塔底液体出口与液化换热器的热流体段接通；这部分结构构成了富甲烷气液化及分离线路；
氮气压缩机的压缩一段、二号中间冷却器、氮气压缩机的压缩二段、二号末级冷却器、预冷换热器的热流体段、冷却换热器的热流体段、液化换热器的热流体段、液氮过冷换热器过冷段依次接通；液氮过冷换热器的过冷段分别与二号塔顶冷凝蒸发器的蒸发段、一号塔顶冷凝蒸发器蒸发段接通；二号塔顶冷凝蒸发器的蒸发段、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、氮气压缩机压缩一段依次接通；一号塔顶冷凝蒸发器的蒸发段、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段氮气压缩机压缩一段依次接通；这部分结构构成了氮气冷剂循环线路。
本实用新型所述的预冷换热器、冷却换热器、液化换热器均为板翅式换热器。
本实用新型与现有技术相比，具有以下优点和效果：传统的混合制冷联合液氮制冷从富甲烷气中制取液化天然气和富氢产品的工艺，精馏塔产生的低温富氢气、富氮气和冷凝器产生的低温氮气以两种方式提供冷量：一种是返回主换热器为所有热流股提供冷量，一种是用于过冷精馏塔底馏出的液化天然气。而本实用新型中，精馏塔产生的低温富氢气体、富氮气体和冷凝器外部液氮蒸发的低温氮气用于过冷来自主换热器的液氮，不同于传统的过冷液化天然气，由于冷流股和热流股的物性更接近，整个换热器过程的冷流体和热流体的换热曲线更匹配，因此换热器冷端温差更小，因此换热效率更高、能耗更低。
附图说明
图1为本实用新型实施例的结构示意图。
具体实施方式
下面结合附图并通过实施例对本实用新型作进一步的详细说明，以下实施例是对本实用新型的解释而本实用新型并不局限于以下实施例。
参见图1，从富甲烷气中制取液化天然气和富氢产品的装置，包括混合冷剂压缩机制冷系统、预冷系统、液化冷箱系统、氮气压缩机系统，及各系统及其设备之间的连接管路。从富甲烷气中制取液化天然气和富氢产品的法，包括混合冷剂循环过程、富甲烷气液化及分离过程、氮气冷剂循环过程。
混合冷剂压缩机制冷系统包括一台电机驱动或蒸汽驱动的混合冷剂压缩机1、一台一号中间冷却器2、一台一号末级冷却器3、一台中间气液分离罐4。混合冷剂压缩机1具有压缩一段和压缩二段。
预冷系统包括一台预冷换热器8、一台冷剂气液分离器11。  
液化冷箱系统包括一台冷却换热器9、一台液化换热器10、一台液氮过冷换热器16、脱氮精馏塔14、脱氢精馏塔17；脱氢精馏塔17的塔顶设有一号塔顶冷凝蒸发器19和一号塔顶气液分离器18；脱氮精馏塔14的塔底设有塔底再沸器15，塔顶设有二号塔顶冷凝蒸发器12和二号塔顶气液分离器13。
氮气压缩机制冷系统包括一台电机驱动或蒸汽驱动的氮气压缩机5、一台二号中间冷却器6、一台二号末级冷却器7。氮气压缩机5具有压缩一段和压缩二段。
混合冷剂循环线路：混合冷剂压缩机1的压缩一段、一号中间冷却器2、中间气液分离罐4、混合冷剂压缩机1的压缩二段、一号末级冷却器3、预冷换热器8的热流体段、冷剂气液分离器11的混合料进口依次接通。冷剂气液分离器11的气体出口、冷却换热器9的热流体段、液化换热器10的热流体段、塔底再沸器15、液化换热器10的热流体段、液化换热器10的冷流体段、冷却换热器9的冷流体段依次接通。冷剂气液分离器11的液体出口、冷却换热器9的热流体段、冷却换热器9的冷流体段依次接通。冷却换热器9的冷流体段与混合冷剂压缩机1的压缩一段接通。
混合冷剂循环过程：由C1～C5和氮气组成的混合工质经过合理配比进入混合冷剂压缩机1入口，经压缩一段压缩至0.8～1.3MPa后进入一号中间冷却器2冷却至30～50℃，再进入中间气液分离罐4进行气液分离；中间气液分离罐4顶部分离出的气体继续进入混合冷剂压缩机1的压缩二段入口，经二段压缩至2.0～4.0MPa后再进入一号末级冷却器3冷却至30～50℃，再进入预冷换热器8热流体段参与换热，被冷却至5～12℃；预冷后的混合工质进入冷剂气液分离器11内进行气液分离，冷剂气液分离器11顶部气体出口出来的气体进入液化冷箱的冷却换热器9的热流体段参与换热，被预冷至-60～-90℃后进入液化换热器10的热流体段，被冷却至-115～-135℃，再进入塔底再沸器15，作为脱氮精馏塔14的热源被冷却至-125～-145℃后返回液化换热器10的热流体段，被冷却至-155～-165℃，再节流至0.23～0.43MPa后返回液化换热器10的冷流体段，为其提供冷量被复热至-65～-95℃。冷剂气液分离器11底部的液体出口出来的液体作为液相冷剂进入液化冷箱的冷却换热器9的热流体段参与换热，在其中被冷却至-60～-90℃，经节流至0.2～0.4MPa后与液化换热器10返回的混合工质流股汇合合并反向进入冷却换热器9的冷流体段，为其提供冷量，复热至5～12℃后再进入混合冷剂压缩机1的压缩一段入口压缩形成混合冷剂循环。
富甲烷气液化及分离线路：预冷换热器8的热流体段、冷却换热器9的热流体段、液化换热器10的热流体段、脱氢精馏塔17进料口依次接通。脱氢精馏塔17的塔顶气体出口、一号塔顶冷凝蒸发器19的冷凝段、一号塔顶气液分离器18进料口依次接通。一号塔顶气液分离器18的液体出口与脱氢精馏塔17的回流液入口接通，一号塔顶气液分离器18的气体出口、液氮过冷换热器16的过冷段、液化换热器10的冷流体段、冷却换热器9的冷流体段、预冷换热器8的冷流体段依次接通。脱氢精馏塔17的塔底液体出口与脱氮精馏塔14的进料口接通。脱氮精馏塔14的塔顶气体出口、二号塔顶冷凝蒸发器12的冷凝段、二号塔顶气液分离器13的进料口依次接通。二号塔顶气液分离器的液体出口与脱氮精馏塔14的回流液入口接通，二号塔顶气液分离器13的气体出口、液氮过冷换热器16的过冷段、液化换热器10的冷流体段、冷却换热器9的冷流体段、预冷换热器8的冷流体段依次接通；脱氮精馏塔14的塔底液体出口与液化换热器10的热流体段接通。
富甲烷气液化及分离过程：净化后的富甲烷气经预冷换热器8预冷至5～12℃后进入液化冷箱的冷却换热器9冷却至-60～-90℃，再进入液化换热器10冷却至-135～-155℃后进入脱氢精馏塔17精馏，脱氢精馏塔17塔顶气体在一号塔顶冷凝蒸发器19中被液氮冷却至-165～-180℃后进入一号塔顶气液分离器18进行气液分离，一号塔顶气液分离器18出来的液体从脱氢精馏塔17顶部的回流液入口返回作为回流液为脱氢精馏塔17提供冷量，一号塔顶气液分离器18顶部分离出的氢气含量85%（体积）以上的富氢气体依次进入液氮过冷器16、液化换热器10、冷却换热器9、预冷换热器8作为返流冷股为换热器提供冷量，最终复热至30～40℃作为富氢产品。脱氢精馏塔17釜液经节流后送入脱氮精馏塔14精馏，脱氮精馏塔14顶部气体在二号塔顶冷凝蒸发器12中被液氮冷却至-165～-180℃后进入二号塔顶气液分离器13进行气液分离，二号塔顶气液分离器13出来的液体从脱氮精馏塔14顶部的回流液入口返回作为回流液为脱氮精馏塔14提供冷量，二号塔顶气液分离器13顶部分离出的的富氮气体依次进入液氮过冷换热器16、液化换热器10、冷却换热器9、预冷换热器8作为返流冷股为换热器提供冷量，最终复热至30～40℃作为富氮产品。脱氮精馏塔14的塔底馏出液为-135～-145℃、甲烷含量≥98%（体积）的液化天然气，返回液化换热器10进行过冷至-160～-170℃，节流后送入LNG储罐储存。
氮气冷剂循环线路：氮气压缩机5的压缩一段、二号中间冷却器6、氮气压缩机5的压缩二段、二号末级冷却器7、预冷换热器8的热流体段、冷却换热器9的热流体段、液化换热器10的热流体段、液氮过冷换热器16过冷段依次接通。液氮过冷换热器16的过冷段分别与二号塔顶冷凝蒸发器12的蒸发段、一号塔顶冷凝蒸发器19蒸发段接通。二号塔顶冷凝蒸发器12的蒸发段、液氮过冷换热器16的过冷段、液化换热器10的冷流体段、冷却换热器9的冷流体段、氮气压缩机5压缩一段依次接通。一号塔顶冷凝蒸发器19的蒸发段、液氮过冷换热器16的过冷段、液化换热器10的冷流体段、冷却换热器9的冷流体段氮气压缩机5压缩一段依次接通。
氮气冷剂循环过程：氮气经氮气压缩机5压缩一段增压至1.0～1.8MPa后经二号中间冷却器6冷却至30～50℃，再进入氮气压缩机5压缩二段增压至3.0～4.0MPa，依次经二号末级冷却器7冷却至30～50℃，预冷换热器8冷却至5～12℃后，再依次进入液化冷箱的冷却换热器9冷却至-60～-90℃，液化换热器10冷却至-150～-165℃，再在液氮过冷换热器16中被返流的低温富氢气体、低温富氮气和低温氮气过冷至-165～-180℃，最后过冷的液氮分别进入脱氮精馏塔14的二号塔顶冷凝蒸发器12、脱氢精馏塔17的一号塔顶冷凝蒸发器19为塔顶气体冷却提供冷量。二号塔顶冷凝蒸发器12和一号塔顶冷凝蒸发器19液氮蒸发后的低温氮气依次经过液氮过冷换热器16、液化换热器10、冷却换热器9回收冷量，复热至7～15℃后进入氮气压缩机5压缩一段再次增压，形成氮气冷剂循环。
冷冻盐水管路：来自溴化锂预冷机组的5～9℃的冷冻盐水作为预冷换热器8的冷股为其提供冷量，被复热至7～12℃出预冷换热器8。
预冷换热器8、冷却换热器9、液化换热器10均为板翅式换热器。
以上所述的各换热器的热流体段中的流体接收冷量，温度降低；冷流体段中的流体提供冷量，温度升高，该概念为本领域的公知常识。
此外，需要说明的是，本说明书中所描述的具体实施例，其零、部件的形状、所取名称等可以不同，本说明书中所描述的以上内容仅仅是对本实用新型结构所作的举例说明。 

Claims (2)

1.一种从富甲烷气中制取液化天然气和富氢产品的装置，其特征在于：包括混合冷剂压缩机制冷系统、预冷系统、液化冷箱系统、氮气压缩机系统；所述的混合冷剂压缩机制冷系统包括混合冷剂压缩机、一号中间冷却器、一号末级冷却器、中间气液分离罐；混合冷剂压缩机具有压缩一段和压缩二段；所述的预冷系统包括预冷换热器、冷剂气液分离器；所述的液化冷箱系统包括冷却换热器、液化换热器、液氮过冷换热器、脱氮精馏塔、脱氢精馏塔；脱氢精馏塔的塔顶设有一号塔顶冷凝蒸发器和一号塔顶气液分离器；脱氮精馏塔的塔底设有塔底再沸器，塔顶设有二号塔顶冷凝蒸发器和二号塔顶气液分离器；所述的氮气压缩机制冷系统包括氮气压缩机、二号中间冷却器、二号末级冷却器；
混合冷剂压缩机的压缩一段、一号中间冷却器、中间气液分离罐、混合冷剂压缩机的压缩二段、一号末级冷却器、预冷换热器的热流体段、冷剂气液分离器的混合料进口依次接通；冷剂气液分离器的气体出口、冷却换热器的热流体段、液化换热器的热流体段、塔底再沸器、液化换热器的热流体段、液化换热器的冷流体段、冷却换热器的冷流体段依次接通；冷剂气液分离器的液体出口、冷却换热器的热流体段、冷却换热器的冷流体段依次接通；冷却换热器的冷流体段与混合冷剂压缩机的压缩一段接通；
预冷换热器的热流体段、冷却换热器的热流体段、液化换热器的热流体段、脱氢精馏塔进料口依次接通；脱氢精馏塔的塔顶气体出口、一号塔顶冷凝蒸发器的冷凝段、一号塔顶气液分离器进料口依次接通；一号塔顶气液分离器的液体出口与脱氢精馏塔的回流液入口接通，一号塔顶气液分离器的气体出口、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、预冷换热器的冷流体段依次接通；脱氢精馏塔的塔底液体出口与脱氮精馏塔的进料口接通；脱氮精馏塔的塔顶气体出口、二号塔顶冷凝蒸发器的冷凝段、二号塔顶气液分离器的进料口依次接通；二号塔顶气液分离器的液体出口与脱氮精馏塔的回流液入口接通，二号塔顶气液分离器的气体出口、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、预冷换热器的冷流体段依次接通；脱氮精馏塔的塔底液体出口与液化换热器的热流体段接通；
氮气压缩机的压缩一段、二号中间冷却器、氮气压缩机的压缩二段、二号末级冷却器、预冷换热器的热流体段、冷却换热器的热流体段、液化换热器的热流体段、液氮过冷换热器过冷段依次接通；液氮过冷换热器的过冷段分别与二号塔顶冷凝蒸发器的蒸发段、一号塔顶冷凝蒸发器蒸发段接通；二号塔顶冷凝蒸发器的蒸发段、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段、氮气压缩机压缩一段依次接通；一号塔顶冷凝蒸发器的蒸发段、液氮过冷换热器的过冷段、液化换热器的冷流体段、冷却换热器的冷流体段氮气压缩机压缩一段依次接通。
2.根据权利要求1所述的从富甲烷气中制取液化天然气和富氢产品的装置，其特征在于：所述的预冷换热器、冷却换热器、液化换热器均为板翅式换热器。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103697659A (zh) * 2013-12-23 2014-04-02 中空能源设备有限公司 从富甲烷气中制取液化天然气和富氢产品的装置及方法
CN113446815A (zh) * 2021-09-01 2021-09-28 杭州制氧机集团股份有限公司 一种采用混合制冷氢气液化设备及其使用方法

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103697659A (zh) * 2013-12-23 2014-04-02 中空能源设备有限公司 从富甲烷气中制取液化天然气和富氢产品的装置及方法
CN103697659B (zh) * 2013-12-23 2015-11-18 中空能源设备有限公司 从富甲烷气中制取液化天然气和富氢产品的装置及方法
CN113446815A (zh) * 2021-09-01 2021-09-28 杭州制氧机集团股份有限公司 一种采用混合制冷氢气液化设备及其使用方法

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