CN101627273A - 由合成气获得产品的方法和设备 - Google Patents

由合成气获得产品的方法和设备 Download PDF

Info

Publication number
CN101627273A
CN101627273A CN200780043967A CN200780043967A CN101627273A CN 101627273 A CN101627273 A CN 101627273A CN 200780043967 A CN200780043967 A CN 200780043967A CN 200780043967 A CN200780043967 A CN 200780043967A CN 101627273 A CN101627273 A CN 101627273A
Authority
CN
China
Prior art keywords
carbon monoxide
gas
condensation
nitrogen
hydrogen
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.)
Pending
Application number
CN200780043967A
Other languages
English (en)
Inventor
M·朗
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 CN101627273A publication Critical patent/CN101627273A/zh
Pending 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
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • 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
    • 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
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • 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
    • C01B2203/047—Composition of the impurity the impurity being 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal 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
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide refrigeration cycle
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

本发明涉及通过在两级冷凝过程中低温分离主要由氢(H2)和一氧化碳(CO)组成的进料气体(1)以获得一氧化碳产品(37)和氢产品(16)的方法，其中通过将富含H2的馏份(43)与液氮(M－N2)(38，42)加以混合而产生第二冷凝级的最大冷量。本发明还涉及用于实施该方法的设备。由以气态从外部输入所述两级冷凝过程的氮(39)通过在所述两级冷凝过程中与待加热的工艺流相对地进行冷却、冷凝和优选过冷而产生M－N2的至少一部分(G－N2)(42)。

Description

由合成气获得产品的方法和设备
技术领域
本发明涉及通过主要由氢(H2)和一氧化碳(CO)组成的进料气体在两级冷凝过程中的低温分离而获得一氧化碳产品和氢产品的方法，其中通过将富含H2的馏份与液氮(M-N2)混合而产生第二冷凝级的最大冷量。本发明还涉及用于实施该方法的设备。
背景技术
通过不同的生产方法，例如催化蒸汽重整或者部分氧化(POX)，由诸如天然气、液化气、石脑油、重油或煤的含烃的原料，产生绝大部分由H2和CO组成的、但还包含甲烷(CH4)、水(H2O)、二氧化碳(CO2)和诸如氮和氩的其他组份的所谓的合成气。由合成气通过提纯和分离特别是获得CO和H2作为产品，它们在工业上有各种各样的用途。
取决于待分离的进料气体的组成、所要求的产品系列和力求达到的产品纯度，特别是采用两种低温分离法、冷凝过程和甲烷洗涤以大规模分离合成气。
两种低温分离法中比较陈旧且比较简单的冷凝过程，特别适合于分离通过部分氧化产生的合成气，因为此类气体通常以高压存在，同时具有高的CO含量和低的甲烷含量。在冷凝过程中，进料气体在与待加热的工艺流相对的间接热交换中进行冷却，从而使其发生部分冷凝，在此形成富含CO、含有H2的液体馏份和富含H2、含有CO的气体馏份，随后在分相器中分离。然后提纯(H2汽提，甲烷分离)其中仍溶解有H2及其他物质的富含CO的液体馏份，并作为CO产品排出。在该方法中，仅能以约90％的产率获得进料气体中所含的CO。此外，产生纯度仅为约90摩尔％的含有H2的物料流，因此无法作为产品排出。
为了避免上述缺点，并以更高的产率获得CO产品，和/或生产纯度大于95摩尔％的H2产品，根据现有技术，冷凝过程围绕膜单元或者围绕冷凝级展开(两级冷凝过程)。在这两个过程中，进一步处理通过冷凝获得的富含H2、含有CO的气体馏份，其中基本上分离出一氧化碳，并导入CO产品中；在分离出一氧化碳之后，富含H2的气体馏份具有所要求的大于95摩尔％的纯度，由此在一些情况下可以省略借助变压吸附的后续纯化。
在两级冷凝过程中，在第一冷凝级获得的富含H2、含有CO的气体馏份与待加热的工艺流相对地进一步冷却，其中产生富含CO、含有H2的第二液体馏份和富含H2、含有CO的第二气体馏份，随后在第二分相器中进行分离。根据现有技术通过将液氮与主要由氢组成的气体馏份加以混合而产生该第二冷凝级所需的最大冷量，为此从外部，例如从低温空气分离机，向低温过程输入液氮，在该低温空气分离机中获得POX所需的氧。为了在第二分离机处达到足够低的温度，必须向两级冷凝过程输入相对大量的液氮，从而使引入的冷量大于满足该过程冷量平衡所需的冷量。目前过剩的冷量未被利用而损失掉。因为以相当大的设备复杂性及特别是能量消耗制备液氮，所以未被利用的冷量显著地损害两级冷凝过程的经济性。
发明内容
因此，本发明的目的在于提出前述类型的方法以及实施该方法的设备，其能够以低于现有技术的运行成本由合成气生产氢产品和一氧化碳产品。
根据本发明在方法方面以如下方式实现该目的，通过在两级冷凝过程中与待加热的工艺流相对地进行冷却、冷凝及优选过冷，由以气态从外部导入两级冷凝过程的氮产生M-N2的至少一部分(G-N2)。
本发明基于以下经验，与液氮相比，可以明显更低的成本生产气态氮。通过采用根据本发明的方法，在空气分离机范围内实现运行成本和投资成本的相应降低。
若将两级冷凝过程例如用于分离通过部分氧化(POX)产生的合成气，并且在空气分离机中通过低温分离空气而获得POX所需的氧，则针对性地从该空气分离机获得液氮。
若冷量平衡表明在两级冷凝过程中无法产生足够的G-N2，以在第二冷凝级的分离机处达到所期望的温度，则根据本发明方法的一个实施方案，以液体形式从外部输入所缺少的氮量(L-N2)。针对性地调节G-N2与L-N2的量的比例，从而以所期望的产率生产一氧化碳产品及以所要求的纯度生产氢产品，但不会发生冷量过剩。
根据本发明方法的另一个实施方案，建议从空气分离机获得G-N2和/或L-N2，在其中生产氧以产生含有氢和一氧化碳的进料气体(例如在POX中)。G-N2优选以中等或低的压力水平从空气分离机排出，从而使该过程的总能量需求最小化。
此外，本发明还涉及用于实施两级冷凝过程的设备(气体分离机)，在其中可将主要由氢(H2)和一氧化碳(CO)组成的进料气体分离成一氧化碳产品和氢产品，其中通过将富含H2的馏份与液氮(M-N2)混合而产生该气体分离机的第二冷凝级的最大冷量。
根据本发明在设备方面以如下方式实现所提出的目的，气体分离机包括用于制造M-N2的至少一部分(G-N2)的装置，在其中将以气态从外部输入的氮通过与待加热的工艺流相对地进行冷却而实施冷凝及优选过冷。
根据现有技术，气体分离机大多具有两个串联的热交换器，其中热交换器是板式热交换器，而第一热交换器的冷侧比第二热交换器的热侧还热。第一热交换器的热侧针对性地经由管道与气态氮的来源相连接，经由该管道可以气态向第一热交换器输入氮。随后在热交换器中与待加热的工艺流相对地对氮进行冷却、冷凝和任选的过冷。
在气体分离机内部没有足够的冷量以从气态氮产生所需M-N2的总量的情况下，根据本发明设备的一个实施方案，该气体分离机装配有一个装置，经由该装置可以从外部以液氮(L-N2)的形式向气体分离机输入一部分量的M-N2。
根据本发明设备的一个优选的实施方案，从空气分离机获得气态氮以产生G-N2和/或L-N2，在其中生产氧以产生含有氢和一氧化碳的进料气体(例如在POX中)。
来自空气分离机的气态氮优选具有中等或低的压力水平。
通过用气态氮代替液氮，根据本发明的方法可以降低用于产生两级冷凝过程中最大冷量的成本，并提高该分离法的经济性。
下面根据两个实施例更详细地阐述本发明，两者均涉及附图中的示意图。
附图说明
图1所示为根据本发明的实施方案。
具体实施方式
该实施例是由含烃的进料生产氢产品和一氧化碳产品的方法。
将含烃的进料1与从空气分离机LZ获得的氧流2一起导入POX反应器P中，在此通过部分氧化转化为主要含有氢(H2)和一氧化碳(CO)的合成粗煤气3。在气体提纯装置R中通过进一步除去诸如水和二氧化碳的非期望的物质而从合成粗煤气3获得主要由氢和一氧化碳组成的进料气体4，随后将其导入低温分离单元Z。在此，通过在两个主热交换器E1和E2中与待加热的工艺流相对地进行冷却和部分冷凝而从进料气体4产生第一两相混合物5，将其在分相器D1中分离成富含H2、含有CO的第一气相6和富含CO、含有H2的第一液相7。在热交换器E3中进一步冷却该富含H2、含有CO的第一气相6，其中所含的一氧化碳的一部分被冷凝出，并产生第二两相混合物8，将其在分相器D2中分离成富含H2、含有CO的第二气相9和富含CO、含有H2的第二液相10。富含CO、含有H2的第二液相10在热交换器E3中与待冷却的工艺流相对地加热之后，经由管道11进一步引导，经由节流装置a减压，与经由节流装置b减压的富含CO、含有H2的第一液相7一起经由管道12引导至H2汽提塔T1，并在塔顶加入。该H2汽提塔T1用于除去溶解于富含CO的物料流12中的氢。使用集成在热交换器E2中的自然循环蒸发器(重沸器)，以加热H2汽提塔T1。从H2汽提塔T1的塔底将物料流13导入重沸器，在此部分蒸发，并经由管道14回流。来自H2汽提塔T1的富含H2、含有CO的塔顶馏份15在热交换器E2和E1中加热，并作为所谓的闪蒸气体16经由气体提纯装置R回流至该过程。若该气体提纯装置R是低温甲醇洗涤(
Figure G2007800439676D00051
)，则优选将在此安装的循环压缩机(未示出)用于该回流。
来自H2汽提塔T1的塔底馏份，即主要含有一氧化碳和氮(N2)的混合物，经由管道17排出，经由节流装置c减压，并送入N2/CO分离塔中。N2/CO分离塔T2直接通过具有产品纯度的一氧化碳19的流18加热，其在中压段V2下游从CO压缩机V排出，在热交换器E1中与待加热的工艺流相对地进行冷却，随后经由节流装置d减压，并直接送入塔底。
将来自N2/CO分离塔T2的塔底的具有产品纯度的一氧化碳馏份27分成两个部分量28和29，其中部分量28经由节流装置g减压，并导入集成于N2/CO分离塔T2中的塔顶冷凝器E5以对其进行冷却，而部分量29在经由节流装置h减压之后与在塔顶冷却器E5中蒸发并从N2/CO分离塔T2的塔顶排出的CO馏份30一起经由管道31流入热交换器E2，将其加热并经由管道32由此排出。为了对低温气体分离过程的冷量预算(
Figure G2007800439676D00052
)进行精细调节，从CO馏份32分流出小的部分量33，并在热交换器E1的旁路中引导，其中通过调节装置i调节部分量33的大小。CO馏份32的剩余的部分量34在热交换器E1中加热，经由管道35进一步引导，并与在旁路中引导的部分量33汇合之后经由管道36作为中间进料送至CO压缩机V。
来自N2/CO分离塔T2塔顶的液态一氧化碳的一部分经由管道20排出。在经由节流装置e减压至低压水平之后，向热交换器E2提供最大冷量，随后在其中蒸发。经由管道21导入热交换器E1，在此加热，并经由管道22导入CO压缩机V第一段V1的吸入侧。
来自N2/CO分离塔T2的塔顶馏份23，即N2/CO混合物，经由节流装置f减压，并导入剩余气体中，其经由管道24和25导入热交换器E1和E2中，并在此加热，然后经由管道26从该过程导出。
两种具有产品品质的一氧化碳馏份22和36在压缩机段V1至V4中压缩至产品压力，并作为CO产品37在设备边缘处排出。
使用两股氮流38和39以产生在两级冷凝过程中所需的最大冷量以及补偿冷量平衡，其中从空气分离机LZ以液态获得一股氮流38，并以气态获得另一股氮流39。还用于回收冷量的气态氮流39首先在热交换器E1和E2中冷却和冷凝，随后经由管道41导入热交换器E3中进行过冷。经由管道42从热交换器E3排出过冷的氮，经由节流装置j减压至剩余气体的压力之后，与来自分离机D2的H2馏份9的部分量43及经由节流装置k导入的液态氮流38混合。通过将液氮与氢混合而使N2/H2混合物44以低于N2露点(78K)的温度于冷侧导入热交换器E3中。由此可以在能够于分离机D2中以高纯度(大于95摩尔％H2)分离出富含H2、含有CO的第二气相9的温度下运行分离机D2。富含H2、含有CO的第二气相9的主要量46在热交换器E3中加热及随后在将其经由管道47和48导入的两个热交换器E2和E1中加热，并作为氢产品49于设备边缘处排出。将在热交换器E3中加热的N2/H2混合物50与来自N2/CO分离塔T2的塔顶馏份23一起导入剩余气体26中。
在第二实施例中，一部分在热交换器E1和E2中冷凝的氮流41用作H2汽提塔T1的回流，以降低富含H2的塔顶馏份中的CO含量。在该构造中，可以省略来自H2汽提塔T1的塔顶馏份16的回流。作为代替，将塔顶馏份15排入剩余气体流24中，或者若要求特别高的H2产率，则在热交换器E3中过冷之后，代替来自分离机D2的富含H2的馏份9的部分流43而与两股液态氮流38和42混合。

Claims (6)

1、通过在两级冷凝过程中低温分离主要由氢(H2)和一氧化碳(CO)组成的进料气体(1)以获得一氧化碳产品(37)和氢产品(16)的方法，其中通过将富含H2的馏份(43)与液氮(M-N2)(38，42)加以混合而产生第二冷凝级的最大冷量，其特征在于，由以气态从外部输入所述两级冷凝过程的氮(39)通过在所述两级冷凝过程中与待加热的工艺流相对地进行冷却、冷凝和优选过冷而产生M-N2的至少一部分(G-N2)(42)。
2、根据权利要求1的方法，其特征在于，M-N2的一部分由G-N2组成，而另一部分(L-N2)从外部以液态导入所述冷凝过程。
3、根据权利要求1或2的方法，其特征在于，由空气分离机获得G-N2和/或L-N2，在该空气分离机中生产氧以产生含有氢和一氧化碳的进料气体。
4、用于实施两级冷凝过程的设备(气体分离机)，在其中将主要由氢(H2)和一氧化碳(CO)组成的进料气体分离成一氧化碳产品和氢产品，其中通过将富含H2的馏份与液氮(M-N2)混合而产生所述气体分离机的第二冷凝级的最大冷量，其特征在于，所述气体分离机包括用于制造M-N2的至少一部分(G-N2)的装置，在其中将以气态从外部输入的氮通过与待加热的工艺流相对地进行冷却而实施冷凝及优选过冷。
5、根据权利要求4的设备，其特征在于，所述气体分离机装配有一个装置，经由该装置从外部以液氮(L-N2)的形式向所述气体分离机输入一部分量的M-N2。
6、根据权利要求4或5的设备，其特征在于，由一个空气分离机获得G-N2和/或L-N2，在其中生产氧以产生含有氢和一氧化碳的进料气体。
CN200780043967A 2006-11-30 2007-11-06 由合成气获得产品的方法和设备 Pending CN101627273A (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006056642A DE102006056642A1 (de) 2006-11-30 2006-11-30 Verfahren und Vorrichtung zur Gewinnung von Produkten aus Synthesegas
DE102006056642.4 2006-11-30

Publications (1)

Publication Number Publication Date
CN101627273A true CN101627273A (zh) 2010-01-13

Family

ID=39338850

Family Applications (1)

Application Number Title Priority Date Filing Date
CN200780043967A Pending CN101627273A (zh) 2006-11-30 2007-11-06 由合成气获得产品的方法和设备

Country Status (4)

Country Link
EP (1) EP2095047A2 (zh)
CN (1) CN101627273A (zh)
DE (1) DE102006056642A1 (zh)
WO (1) WO2008064762A2 (zh)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103438666A (zh) * 2013-08-21 2013-12-11 张周卫 低温液氮用多股流缠绕管式主回热换热装备
CN110044133A (zh) * 2019-05-17 2019-07-23 成都赛普瑞兴科技有限公司 分离提纯一氧化碳的设备与方法

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3018599B1 (fr) * 2014-03-17 2019-06-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation cryogenique d’un gaz de synthese contenant du monoxyde de carbone, du methane et de l’hydrogene
DE102014015160A1 (de) 2014-10-14 2016-04-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Kohlenmonoxid und Wasserstoff aus Synthesegas
FR3075067B1 (fr) * 2017-12-14 2020-08-28 Air Liquide Procede et appareil de separation cryogenique d'un gaz de synthese contenant une etape de separation de l'azote
WO2023139259A1 (en) * 2022-01-24 2023-07-27 Topsoe A/S Effective use of cryogenic separation section in syngas manufacture

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1515926A (fr) * 1966-09-30 1968-03-08 Air Liquide Procédé de production d'oxygène et d'azote pur sous pression élevée à partir d'air en vue de la fabrication et de la purification à basse température d'un mélange d'hydrogène et d'azote
IN160585B (zh) * 1983-02-14 1987-07-18 Exxon Research Engineering Co
DE3802552A1 (de) * 1988-01-28 1989-08-10 Linde Ag Verfahren zum reinigen eines gasgemisches
GB9802231D0 (en) * 1998-02-02 1998-04-01 Air Prod & Chem Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures also containing hydrogen
ATE289047T1 (de) * 2000-12-18 2005-02-15 Air Prod & Chem Verfahren und vorrichtung zur abtrennung von kohlenmonoxid und wasserstoff aus einem gasgemisch
DE10226209B4 (de) * 2002-06-13 2008-04-03 Lurgi Ag Anlage und Verfahren zur Erzeugung und Zerlegung von Synthesegasen aus Erdgas
DE10226210A1 (de) * 2002-06-13 2004-01-08 Lurgi Ag Anlagenteil zur Zerlegung und Reinigung von Synthesegas
DE102005046790A1 (de) * 2005-09-29 2007-04-05 Linde Ag Verfahren zur Reinigung eines Gasgemisches

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103438666A (zh) * 2013-08-21 2013-12-11 张周卫 低温液氮用多股流缠绕管式主回热换热装备
CN110044133A (zh) * 2019-05-17 2019-07-23 成都赛普瑞兴科技有限公司 分离提纯一氧化碳的设备与方法
CN110044133B (zh) * 2019-05-17 2024-03-22 成都赛普瑞兴科技有限公司 分离提纯一氧化碳的设备与方法

Also Published As

Publication number Publication date
EP2095047A2 (de) 2009-09-02
DE102006056642A1 (de) 2008-06-05
WO2008064762A2 (de) 2008-06-05
WO2008064762A3 (de) 2009-04-23

Similar Documents

Publication Publication Date Title
CN102007358B (zh) 深冷分离氢气和一氧化碳的混合物的方法和设备
CN100519406C (zh) 从合成气中除去氮、甲烷和氩用低△p净化器
CN109690215A (zh) 工业气体场所与液氢生产的一体化
CN101680713B (zh) 通过低温蒸馏分离包含一氧化碳、甲烷、氢和可选的氮的混合物的方法
CN101650112B (zh) 组合的合成气分离和lng生产方法及***
US8591770B2 (en) Process for the production of syngas for ammonia synthesis
CN107328166B (zh) 一种采用双循环的co深冷分离***及其分离方法
RU2558579C2 (ru) Производство кондиционного синтез-газа для синтеза аммиака с криогенной очисткой
RU2011140704A (ru) Разделение диоксида углерода и водорода
CN101627273A (zh) 由合成气获得产品的方法和设备
KR102217256B1 (ko) 일산화탄소를 생성하는 방법 및 장치
KR101265916B1 (ko) 합성 가스의 극저온 분리
CN101782308A (zh) 煤气化装置来原料气甲烷深冷分离装置的换热***
CN101528648A (zh) 用于gtl装置的轻烃回收方法
CA2262047A1 (en) Process and plant for the combined production of an ammonia synthesis mixture and carbon monoxide
CN101568788B (zh) 通过低温蒸馏分离至少包含氢、氮和一氧化碳的混合物的方法和设备
CN113862051A (zh) 双制冷循环甲烷洗合成气深冷分离装置及分离方法
CN108055839B (zh) 用于生产一氧化碳和氢气的混合物的方法和设备
CN106871576B (zh) 工业合成气低温前脱甲烷方法及***
CN109477683A (zh) 用于分离合成气的方法
JP3923766B2 (ja) 水素製造装置
CN108431184B (zh) 在气体减压站制备天然气以生产液体天然气(lng)的方法
CN208635425U (zh) 一种利用液化天然气冷能的中间进料焦炉煤气回收***
CN102502702A (zh) 以天然气为原料制备氨的方法
US20190128601A1 (en) Process and plant for the combination production of a mixture of hydrogen and nitrogen and also of carbon monoxide by cryogenic distillation and cryogenic scrubbing

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C02 Deemed withdrawal of patent application after publication (patent law 2001)
WD01 Invention patent application deemed withdrawn after publication

Open date: 20100113