CN109963810A - 使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和装置 - Google Patents

使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和装置 Download PDF

Info

Publication number
CN109963810A
CN109963810A CN201780071227.7A CN201780071227A CN109963810A CN 109963810 A CN109963810 A CN 109963810A CN 201780071227 A CN201780071227 A CN 201780071227A CN 109963810 A CN109963810 A CN 109963810A
Authority
CN
China
Prior art keywords
gas
cryogenic
carbon monoxide
synthesis gas
nitrogen
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.)
Granted
Application number
CN201780071227.7A
Other languages
English (en)
Other versions
CN109963810B (zh
Inventor
M·朗
F·阿尔贝特
K·吉泽
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Publication of CN109963810A publication Critical patent/CN109963810A/zh
Application granted granted Critical
Publication of CN109963810B publication Critical patent/CN109963810B/zh
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • 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
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis 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
    • 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
    • F25J3/0261—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 carbon monoxide
    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
    • 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
    • F25J2270/90—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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

本发明涉及一种用于粗合成气(4)的分馏的方法和装置，其中从所述粗合成气(4)中分离二氧化碳和硫组分到酸性气体洗涤器(M)中，以获得主要由氢气和一氧化碳组成的含甲烷的合成气(6)，随后在低温分离过程(T)中由所述含甲烷的合成气(6)获得一氧化碳产物(9)，其中在所述酸性气体洗涤器(M)中使用第一压力水平的汽提气体(14)，所述汽提气体(14)通过具有比所述第一压力水平高的第二压力水平的氮源(L)获得。其特征在于，由所述氮源(L)提供的气体(12)在所述低温分离过程(T)中被用作制冷剂(13)，并且因此被减压至所述第一压力水平，以随后被供应至酸性气体洗涤器(14)作为汽提气体(14)。

Description

使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和 装置
本发明涉及一种用于粗合成气的分馏的方法，在酸性气体洗涤器中从所述粗合成气中分离出二氧化碳和硫组分，以获得主要由氢气和一氧化碳组成的含甲烷的合成气，随后在低温分离过程中由所述含甲烷的合成气获得一氧化碳产物，其中在所述酸性气体洗涤器中，在第一压力水平下使用汽提气体，所述汽提气体通过具有比所述第一压力水平高的第二压力水平的氮源而获得。
本发明还涉及一种用于实施本发明方法的装置。
在本申请中，术语"压力水平"和"温度水平"用来表征压力和温度，以便表达用于执行根据本发明的方法的参数不必具有精确值的想法。而是，它们近似为平均值。相应的水平位于不连贯的范围内。
与物种相关的方法和装置例如用于由煤生产单乙二醇。在这种情况下，在引入氧气的情况下，通过部分氧化将煤转化为粗合成气，其中除了主要成分氢气和一氧化碳之外，粗合成气还含有酸性气体，特别是二氧化碳和硫组分，以及水和甲烷。冷却和干燥后，将粗合成气通入酸性气体洗涤器，在其中借助于甲醇洗涤剂分离酸性气体，其中得到主要由氢气和一氧化碳组成的含甲烷的合成气和负载有分离的酸性气体的洗涤剂。为了能够在酸性气体分离过程中重复使用，再生该负载的洗涤剂，在这个过程中通过用作汽提气体的氮气，通常在1.5-3巴(a)的压力下，将酸性气体除去。
为了避免凝华，在低温冷凝过程中将合成气分解产生一氧化碳产物和粗氢气之前，在变温吸附器中从所述合成气中除去痕量的酸性气体和洗涤剂残余物。粗氢气通常用于再生变温吸附器，然后通过变压吸附将其纯化以产生氢气产物，然后与一氧化碳产物一起反应以形成单乙二醇。
煤气化所需的氧气由低温空气分离单元提供，该单元同时还提供氮气作为用于酸性气体洗涤器的汽提气体。氮气通常在4-6巴(a)的压力下在空气分离单元中以气相形成，因此在用于酸性气体洗涤器之前必须减压。为了减压，将氮气通过节流元件，其中压能大量损失，没有经济效益。
因此，本发明的目的是提供在引言中描述的方法和装置，利用该方法和装置可以克服相关技术的缺点。
根据本发明，所述目的由以下方法得以实现：在所述方法中由氮源提供的气体在低温分离过程中被用作制冷剂，并且在该过程中被减压至第一压力水平，使得其随后可以作为汽提气体被供给至酸性气体洗涤器。
利用根据本发明的方法，可以使打算用作汽提气体的氮气还用以在低温单元中执行制冷剂的功能，并且从在相关技术中未被使用的来自氮源的用作汽提气体的气体中的压能满足用于操作低温分离过程所需的能量的至少一部分，因此有利地使用它。当由氮源提供的气体用作制冷剂时，其化学组成没有改变，因此不需要进行任何进一步的处理以使其在酸性气体洗涤器中可用作汽提气体。
一氧化碳产物的压力水平决定了来自氮源的气体必须作为制冷剂供给到低温分离过程的压力水平的最小值。特别地，如果第二压力水平没有达到该最小值，则建议在将由氮源供应的气体引入到低温分离过程中之前，将其从第二压力水平压缩到等于或大于所述最小值的第三压力水平。
被供应到低温分离过程中并在其中用作制冷剂的来自氮源的气体的量优选等于酸性气体洗涤器中所需的汽提气体的量，并且在被减压到第一压力水平之后，将其全部供给到酸性气体洗涤器。然而，这并不排除比所需汽提气体量更多或更少量的来自氮源的气体作为致冷剂被供应到低温分离过程中。
如果在用于低温分离过程之前将氮气从第二压力水平压缩至第三压力水平，并且用作制冷剂的氮气的量超过在第一压力水平下输送的气体的量，则建议当其在低温分离过程中用作制冷剂时将过量的气体量仅减压至第二压力水平，并且在再次压缩至第三压力水平之后作为制冷剂返回至冷凝过程。
另一方面，如果在酸性气体洗涤器中对汽提气体的需要不能完全从低温分离过程中得到满足，则不足量可以方便地直接由氮源提供，其中将氮气通过节流元件从第二压力水平减压至第一压力水平。如果作为制冷剂供应的来自氮源的气体所产生的冷却能量不足以进行低温分离过程，则可以另外使用液氮作为制冷剂。
如果所述低温分离过程是冷凝工艺，则实施本发明的方法是特别有利的。
冷凝工艺已经是相关技术的一部分，并且为专业团体所知已有多年。它优选用于通过部分氧化获得的并因此具有高的一氧化碳含量和低的甲烷含量的合成气的分馏。通过冷却将合成气部分冷凝以获得主要由一氧化碳和甲烷组成的含氢第一液相，通过在H2汽提塔中分离氢而由该含氢第一液相产生第二液相，并且在CO/CH4分离塔中由该第二液相获得纯度足以作为一氧化碳产物输送的富含一氧化碳的气相和主要由甲烷和一氧化碳组成的塔底产物。如果将待分馏的合成气冷却到足够低的温度，则在冷凝过程中，可以以大于85％的收率生产一氧化碳产物，该一氧化碳产物具有小于100vppm的甲烷含量，因此可以在没有任何进一步纯化步骤的情况下用以制造例如单乙二醇。
为了可以获得特别对于低温分离过程所需的最大制冷量(refrigerationcapacity)，并且为了在CO/CH4塔的顶部产生回流，根据相关技术，使用通过循环压缩机驱动的制冷循环，其中外部供应的氮或内部产生的一氧化碳作为制冷剂循环。
两个制冷循环都通过多级压缩机驱动。而在氮循环中，可以使用相对便宜的两级压缩机，一氧化碳压缩机需要高得多的成本。其原因首先是因为一氧化碳压缩机必须配置有至少三个压缩机级，以避免一氧化碳的热分解和由此产生的烟灰沉积物。其次，它必须是防爆的，必须在特别安全的区域中操作，以防止逃逸的一氧化碳伤害人们或损坏设备。因此，用于驱动一氧化碳循环的压缩机比设计用于相应的氮循环的压缩机成本高了多达50％。
根据本发明的方法使得可以用比现有技术更简单、更便宜的压缩机和更低的操作成本来操作冷凝过程的制冷剂循环，因为来自氮源的气体已经在较高的压力下供应，因此需要经受更少的额外压缩。除了由氮源供应的气体的压缩程度之外，压缩机的构造还受到第三压力水平的强度的影响，第三压力水平的强度又主要取决于冷凝过程内的过程控制。上述类型的冷凝过程已经被确认特别有利于这些目的，其中CO/CH4分离塔利用用作制冷剂的氮气和至少一部分待分馏的合成气加热，其中第二液相被分成第一、第二和第三分流，其中第一分流靠在CO/CH4分离塔加热期间冷却的冷凝氮气蒸发，第二分流靠部分冷凝的合成气蒸发，并且由此形成的蒸气相作为中间加热供给到CO/CH4分离塔，而第三分流作为中间回流排放到CO/CH4分离塔。
冷凝过程的一氧化碳产率基本上取决于最大制冷量的可达到温度水平，该水平由第一压力水平决定。由于使用氮气作为制冷剂，因此2至3巴(A)的第一压力水平已经足以获得与使用相当昂贵的一氧化碳制冷循环获得的产量相当的产量。
在这种冷凝过程中，用作制冷剂的氮气优选被减压小于13巴，特别优选被减压小于10巴，以达到第一压力水平。
本发明还涉及一种用于粗合成气分馏的装置，其具有酸性气体洗涤器，用于通过从所述粗合成气中分离二氧化碳和硫组分并使用处于第一压力水平的汽提气体获得主要由氢气和一氧化碳组成的含甲烷的合成气；低温气体分馏单元，其中可以从所述合成气获得一氧化碳产物；和氮源，其中可以在高于第一压力水平的第二压力水平下从所述氮源中提出汽提气体。
所述目的通过根据本发明的以下装置来实现：其中低温气体分馏单元连接到酸性气体洗涤器和氮源，使得气体可以从氮源供应到所述低温气体分馏单元，从而该低温气体分馏单元能够使用该气体作为制冷剂，并且随后将其作为减压到第一压力水平的汽提气体输送到酸性气体洗涤器。
在优选的变体中，根据本发明的装置包括压缩机，该压缩机连接到氮源和低温气体分馏单元，在作为制冷剂从氮源获取的气体被引入到低温气体分馏单元之前，通过该压缩机将该气体压缩到第三压力水平。
低温气体分馏单元特别优选设计成进行冷凝过程，为此，它包括至少一个用于冷却和部分冷凝合成气的热交换器；分离器，在该分离器中第一液相可以从部分冷凝的合成气中分离；H2汽提塔，其中通过分离氢可以由所述第一液相产生第二液相；以及CO/CH4分离塔，其与作为制冷循环的一部分的再沸器连接，并且通过该分离塔可以从包含在制冷循环中的氮和要分馏的合成气的一部分中提取热量并将该热量供给到CO/CH4分离塔以加热它，从而从所述第二液相获得具有可以作为一氧化碳产物排出的纯度的富一氧化碳气相和主要由甲烷和一氧化碳组成的塔底产物，其中第二液相可以分成第一、第二和第三分流，其中第一分流可以靠CO/CH4分离塔加热期间冷却的冷凝氮蒸发，第二分流可以靠部分冷凝的合成气蒸发，并且由此形成的气相可以作为中间加热被供应到CO/CH4分离塔，而第三分流可以作为中间回流被排放到CO/CH4分离塔。
为了提供特别优选的低温气体分馏单元，从氮源取得并用作制冷剂的气体仅需要相对低的第三压力水平，在第一压力水平之上不超过13巴，因此如果第二压力水平比第一压力水平高至少2巴，则可以简单地使用单级压缩机来实现压缩。
氮源优选为低温空气分离单元，其能够提供压力为4-6巴(a)的气相氮。
酸性气体洗涤器也优选实施为甲醇洗涤器，其中压力水平为1.5-3巴(a)的氮气可以用作洗涤剂再生的汽提气体。
在下文中，将参考图1和2中图解表示的本发明的两个实施方案更详细地解释本发明。
图1显示单乙二醇的产生，其中粗合成气以本发明的方式分馏。
图2显示了根据冷凝过程操作的低温分离装置，当实施本发明的方法时，可以有利地使用该装置。
在图1中，含碳原料如煤或重油通过管线1被进料到反应器R中，在反应器R中，其与来自低温空气分离单元L的氧气2通过部分氧化反应形成粗合成气，该粗合成气在除去烟灰后通过管线3进入合成气冷却器K。冷却和干燥后，粗合成气4被送入酸性气体洗涤器M，在其中借助于甲醇洗涤剂分离二氧化碳和其它酸性气体，其中得到主要由氢气和一氧化碳组成的含甲烷的合成气5和负载有分离的酸性气体的洗涤剂。为了避免在随后的工艺步骤中凝华，在将合成气5通过管线6进料到低温分离装置T之前，在变温吸附器A中将剩余的痕量酸性气体和洗涤剂残余物从合成气5中分离，所述低温分离装置T优选以冷凝工艺操作。在低温分离装置T中获得的粗氢气7首先在变温吸附器A中用作再生气体，然后在变压吸附器D中纯化以得到氢产物8，该氢产物在合成单元G中与同样在低温分离装置T中产生的一氧化碳产物9一起反应以形成单乙二醇10。除了部分氧化所需的氧气2之外，低温空气分离单元L输送液体11以满足低温分离装置T的制冷需要，并且输送压力水平为4-6巴(a)的气相氮12，该气相氮12需要在酸性气体洗涤器M中的进料甲醇洗涤剂的再生中作为汽提气体。在用作汽提气体之前，气相氮12借助于优选单级压缩机P进一步压缩到12-16巴(a)的值，并作为制冷剂13引入到低温分离装置T的制冷循环中，在那里它被减压具有冷却效果以提供大部分必要的制冷量。减压的氮气14在汽提气体的压力水平下离开低温分离装置T，并被送至酸性气体洗涤器M。如果在低温分离装置T中可以使用比在酸性气体洗涤器M中作为汽提气体所需的更少的氮气作为制冷剂，则气相氮12的一部分15在压缩机P的上游被转移出低温空气分离单元L，并且在其也作为汽提气体被供应到酸性气体洗涤器M之前经过节流元件a被减压。
在图2所示的低温分离装置T中，已经在变温吸附器A中纯化的合成气6在第一热交换器E1中被冷却而不靠在30-60巴(A)的压力下待加热的工艺流冷凝，然后被分成第一分流22和第二分流23，在再沸器R中从第一分流22中提取热量以加热CO/CH4分离塔T2，产生进一步冷却的完全气态的第一分流24，与在旁路中被送到再沸器R的第二分流23合并以形成合成气流25。可以改变这两个分流22和23的量比，以控制CO/CH4分离塔T2中的温度条件。
在第二热交换器E2中，合成气流25被冷却，直到通过组分的冷凝形成两相物质混合物26，该混合物在分离器B中被分离成主要由一氧化碳和甲烷组成的含氢液相和富氢气相。所述气相通过管线27从分离器B中提取，并且在热交换器E2和E1中加热之后，在被送至变压吸附器D之前，作为粗氢气7用以再生变温吸附器A。另一方面，液相29被供给到H2分离塔T1。为此，将其分成两个分流，其中第一分流30被减压回流至H2分离塔T1的塔顶，而第二分流31在经过减压和随后在热交换器E2中部分蒸发之后作为中间加热而排放到H2分离塔T1的中部。
在等于合成气6压力的1/5-1/3的压力下操作的H2分离塔T1用于除去溶解在液相29中的氢。它由集成在热交换器E2中的循环加热器32加热。
在热交换器E2和E1中加热之后，来自H2分离塔T1的富氢的塔顶馏分33在系统边界处作为闪蒸气体28排出，而由一氧化碳和甲烷组成的基本上不含氢的塔底馏分35被分成三个分流36、37和38，并且被送至CO/CH4分离塔T2中减压，该分离塔在5-10巴(a)的压力下操作。CO/CH4分离塔T2经再沸器R加热，其中至少一部分再沸器物流39被蒸发。
低温分离过程所需的最大制冷量通过由压缩机P驱动的制冷剂回路获得，其中由低温气体分馏单元L以气相提供的氮12作为制冷剂循环。氮气13在比酸性气体洗涤器M中所需的汽提气体压力大不超过13巴的压力下离开优选单级压缩机P，然后在热交换器E1中冷却，并在再沸器R中进一步冷却，而不靠来自CO/CH4分离塔T2的再沸器物流39与合成气6的第一分流22一起冷凝。在热交换器E3中，已经在再沸器R中冷却的氮40靠分流36冷凝，所述分流36通常占H2分离塔T1的塔底馏分35的量的超过45％，随后蒸发并作为气流42输送。塔底馏分35的第二分流37也在热交换器E2中靠待部分冷凝的合成气流25蒸发，并且作为气流43与气流42合并以形成气流44，然后通入CO/CH4分离塔T2作为中间加热。塔底馏分35的第三分流38仅占总量的约5-10％，在减压后作为中间回流排放到CO/CH4分离塔T2。
在热交换器E3中冷凝的氮41的一部分45被减压，产生制冷量到达CO/CH4分离塔T2的顶部，在那里设置冷凝器C并通过液氮冷却该冷凝器以输送温差来驱动塔内的一氧化碳回流46。来自CO/CH4分离塔T2的塔顶的冷凝氮41的第二部分47和气相氮48各自减压至酸性气体洗涤器中所需的汽提气体的压力水平，产生制冷量，并与双相氮流49合并，为热交换器E2的冷端提供最大制冷量。在热交换器E2和E1中蒸发和加热之后，氮49作为汽提气体14被供应到酸性气体洗涤器M。
在冷凝器C下方，具有产品纯度的一氧化碳馏分50从CO/CH4分离塔T2中排出，并且在热交换器E2和E1中加热之后，作为一氧化碳产品9被送至单乙二醇合成单元G而不进一步压缩。
额外的制冷量通过氮11引入分离过程，氮11以液体形式从低温空气分离单元L中抽出，并且在热交换器E2和E1中蒸发和加热后，作为气相通过管线51排放到大气或火炬系统中。
在CO/CH4分离塔T2的塔底空间S中收集也在热交换器E2和E1中蒸发和加热的富含甲烷的含一氧化碳的液相52，然后将其作为燃料气体53排出。

Claims (10)

1.一种用于粗合成气(4)的分馏的方法，其中从所述粗合成气(4)中分离二氧化碳和硫组分到酸性气体洗涤器(M)中，以获得主要由氢气和一氧化碳组成的含甲烷的合成气(6)，随后在低温分离过程(T)中由所述含甲烷的合成气(6)获得一氧化碳产物(9)，其中在所述酸性气体洗涤器(M)中使用第一压力水平的汽提气体(14)，所述汽提气体(14)通过具有比所述第一压力水平高的第二压力水平的氮源(L)获得，其特征在于，由所述氮源(L)提供的气体(12)在所述低温分离过程(T)中被用作制冷剂(13)，并且由此被减压至所述第一压力水平，以随后被供应至所述酸性气体洗涤器作为汽提气体(14)。
2.根据权利要求1的方法，其特征在于，由所述氮源(L)提供的作为制冷剂的气体(12)在被引入到所述低温分离过程(T)之前被压缩到第三压力水平。
3.根据权利要求2的方法，其特征在于，不需要在所述酸性气体洗涤器(M)中作为汽提气体并且在所述低温分离过程(T)中用作制冷剂(13)的氮气仅被减压到所述第二压力水平，并且在压缩到所述第三压力水平之后作为制冷剂返回到冷凝过程。
4.根据权利要求1-3中任一项的方法，其特征在于，所述合成气(6)在所述低温分离过程中通过冷却被部分冷凝，得到主要由一氧化碳和甲烷组成的第一含氢液相(29)，由所述第一含氢液相(29)通过在H2汽提塔(T1)中分离氢而产生第二液相(35)，所述第二液相(35)在CO/CH4分离塔(T2)中被分离成具有可以作为一氧化碳产物(9)排出的纯度的富含一氧化碳的气相(50)，和主要由甲烷和一氧化碳组成的塔底产物(52)，所述CO/CH4分离塔(T2)通过用作制冷剂的氮气(13)和合成气(6)的至少一部分(22)加热，其中所述第二液相(35)被分成第一分流(36)、第二分流(37)和第三分流(38)，其中所述第一分流(36)靠CO/CH4分离塔(T2)加热期间冷却的冷凝氮(40)蒸发，所述第二分流(37)靠部分冷凝的合成气(25)蒸发，并且由此形成的气相(42，43)作为中间加热被供给到CO/CH4分离塔(T2)，而所述第三分流(38)作为中间回流被排放到CO/CH4分离塔(T2)。
5.根据权利要求4的方法，其特征在于，在所述低温分离过程(T)中，用作制冷剂的氮气(13)被减压小于13巴，优选小于10巴，以达到所述第一压力水平。
6.一种用于粗合成气(4)的分馏的装置，其具有酸性气体洗涤器(M)，所述酸性气体洗涤器用于通过从所述粗合成气中分离出二氧化碳和硫组分并使用第一压力水平的汽提气体(14)而获得主要由氢气和一氧化碳组成的含甲烷的合成气(6)；低温气体分馏单元(T)，在所述低温气体分馏单元(T)中可以从所述合成气(6)中获得一氧化碳产物(9)；和氮源(L)，由所述氮源(L)可以在高于第一压力水平的第二压力水平下抽出汽提气体(12)，其特征在于，所述低温气体分馏单元(T)与所述酸性气体洗涤器(M)和氮源(L)连接，使得可以由所述氮源(L)向该低温气体分馏单元(T)提供气体(12)，以便所述气体(12)可以用作制冷剂，并且随后在减压至第一压力水平之后作为汽提气体(14)排出到所述酸性气体洗涤器中。
7.根据权利要求6的装置，其特征在于，它包括与所述氮源(L)和低温气体分馏单元(T)连接的压缩机(P)，通过所述压缩机，由氮源提供的作为制冷剂的气体(12)在被引入低温气体分馏单元(T)之前可被压缩至第三压力水平。
8.根据权利要求7的装置，其特征在于，所述低温气体分馏单元(T)包括至少一个用于冷却和部分冷凝所述合成气(25)的热交换器(E2)；分离器(B)，在所述分离器(B)中可以从部分冷凝的合成气(26)中分离出第一液相(29)；H2汽提塔(T1)，在所述H2汽提塔(T1)可通过分离氢由所述第一液相(29)产生第二液相(35)；以及CO/CH4分离塔(T2)，所述CO/CH4分离塔(T2)与再沸器(R)连接，所述再沸器(R)是制冷循环的一部分，并且通过该再沸器可以从进入制冷循环的氮气(13)以及从要分馏的合成气(6)的一部分(22)中提取热量并供给到CO/CH4分离塔(T2)以加热它，从而由所述第二液相(35)获得足够纯的富含一氧化碳的气相(50)以使其能够作为一氧化碳产物(9)输出，和获得主要由甲烷和一氧化碳组成的塔底产物(52)，其中所述第二液相(35)可以分成第一分流(36)、第二分流(37)和第三分流(38)，其中所述第一分流(36)可以靠CO/CH4分离塔(T2)加热期间冷却的冷凝氮(40)蒸发，所述第二分流(37)可靠部分冷凝的合成气(25)蒸发，并且由此形成的气相(42，43)可作为中间加热供给到CO/CH4分离塔(T2)，而所述第三分流(38)可以作为中间回流排放到CO/CH4分离塔(T2)。
9.根据权利要求8所述的装置，其特征在于，所述压缩机(P)是单级设计的。
10.根据权利要求6-8中任一项的装置，其特征在于，所述氮源(L)是低温空气分离单元。
CN201780071227.7A 2016-11-18 2017-11-08 使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和装置 Active CN109963810B (zh)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102016013753.3 2016-11-18
DE102016013753.3A DE102016013753A1 (de) 2016-11-18 2016-11-18 Verfahren und Vorrichtung zur Synthesegaszerlegung mittels Sauergaswäsche und kryogenem Trennprozess
PCT/EP2017/025324 WO2018091146A1 (de) 2016-11-18 2017-11-08 Verfahren und vorrichtung zur synthesegaszerlegung mittels sauergaswäsche und kryogenem trennprozess

Publications (2)

Publication Number Publication Date
CN109963810A true CN109963810A (zh) 2019-07-02
CN109963810B CN109963810B (zh) 2023-01-24

Family

ID=60421727

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201780071227.7A Active CN109963810B (zh) 2016-11-18 2017-11-08 使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和装置

Country Status (3)

Country Link
CN (1) CN109963810B (zh)
DE (1) DE102016013753A1 (zh)
WO (1) WO2018091146A1 (zh)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3097951B1 (fr) * 2019-06-26 2022-05-13 Air Liquide Procede et appareil de separation cryogenique d’un gaz de synthese pour la production de ch4
EP3851179A1 (en) * 2020-01-14 2021-07-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for separating a synthesis gas by cryogenic distillation

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2718725A1 (fr) * 1994-04-13 1995-10-20 Air Liquide Procédé et installation de séparation d'un mélange gazeux.
CN1237535A (zh) * 1998-02-20 1999-12-08 液体空气乔治洛德方法利用和研究有限公司 生产一氧化碳和氢的方法和设备
CN1907850A (zh) * 2005-06-03 2007-02-07 林德股份公司 从合成气中得到产品的方法和装置
EP2311544A1 (en) * 2009-10-05 2011-04-20 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for the treatment of a synthesis gas
CN103328375A (zh) * 2011-01-17 2013-09-25 乔治洛德方法研究和开发液化空气有限公司 使用低温分离生产氨合成气和纯甲烷的方法和装置

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6416568B1 (en) * 1999-05-14 2002-07-09 Texaco, Inc. Hydrogen recycle and acid gas removal using a membrane
DE102005021530A1 (de) * 2005-05-10 2006-11-23 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Produkten aus Synthesegas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2718725A1 (fr) * 1994-04-13 1995-10-20 Air Liquide Procédé et installation de séparation d'un mélange gazeux.
CN1237535A (zh) * 1998-02-20 1999-12-08 液体空气乔治洛德方法利用和研究有限公司 生产一氧化碳和氢的方法和设备
CN1907850A (zh) * 2005-06-03 2007-02-07 林德股份公司 从合成气中得到产品的方法和装置
EP2311544A1 (en) * 2009-10-05 2011-04-20 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for the treatment of a synthesis gas
CN103328375A (zh) * 2011-01-17 2013-09-25 乔治洛德方法研究和开发液化空气有限公司 使用低温分离生产氨合成气和纯甲烷的方法和装置

Also Published As

Publication number Publication date
CN109963810B (zh) 2023-01-24
WO2018091146A1 (de) 2018-05-24
DE102016013753A1 (de) 2018-05-24

Similar Documents

Publication Publication Date Title
US4305733A (en) Method of treating natural gas to obtain a methane rich fuel gas
US3498067A (en) Systems for removal of co2 from gaseous mixtures
US8641802B2 (en) Method for treating a process gas flow containing CO2
JP3917198B2 (ja) 一酸化炭素の製造方法及びその製造プラント
JPH0624705A (ja) 高純度水素と高純度一酸化炭素の製造方法
JPS6362675B2 (zh)
CN102245500B (zh) 由重整气体生产氢并同时捕捉共产生的co2
US1913805A (en) Process for separating gas mixtures more particularly coke oven gas
US3910777A (en) Absorption system for separate recovery of carbon dioxide and hydrogen sulfide impurities
JPS58195778A (ja) 一酸化炭素の製造方法
US20220144634A1 (en) Process and plant for producing hydrogen and for separating carbon dioxide from synthesis gas
CN107438475B (zh) 从吸收剂中能量有效回收二氧化碳的方法和适于运行该方法的设备
ATE544040T1 (de) Verfahren und vorrichtung zur gewinnung von produkten aus synthesegas
CN103123203A (zh) 利用含氮废气进行再低温精馏制取纯氮的方法
ATE548618T1 (de) Verfahren und vorrichtung zur gewinnung von produkten aus synthesegase
US2284662A (en) Process for the production of krypton and xenon
US1773012A (en) Process for the separation of gas mixtures
JPH0972656A (ja) アルゴン精製方法及び装置
CN109963810A (zh) 使用酸性气体洗涤和低温分离工艺进行合成气分馏的方法和装置
US3074245A (en) Process for the selective removal of carbon dioxide and hydrogen sulfide from gaseous mixtures containing the same
NL2015921B1 (en) Process for the purification of a gas
CA2783049A1 (en) Method and device for scrubbing medium regeneration in gas scrubbers
US20160146534A1 (en) Method for recovering an ethylene stream from a carbon monoxide rich feed stream, and associated installation
CN108055839B (zh) 用于生产一氧化碳和氢气的混合物的方法和设备
US11826694B2 (en) Process and plant for removing carbon dioxide from synthesis gas

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant