AU2019272028A1 - Process and apparatus for separating a feed stream comprising at least co2 and also at least one light component - Google Patents

Process and apparatus for separating a feed stream comprising at least co2 and also at least one light component Download PDF

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Publication number
AU2019272028A1
AU2019272028A1 AU2019272028A AU2019272028A AU2019272028A1 AU 2019272028 A1 AU2019272028 A1 AU 2019272028A1 AU 2019272028 A AU2019272028 A AU 2019272028A AU 2019272028 A AU2019272028 A AU 2019272028A AU 2019272028 A1 AU2019272028 A1 AU 2019272028A1
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fluid
gas
distillation column
feed stream
permeate
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AU2019272028A
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AU2019272028B2 (en
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Oumar KHAN
Mathieu LECLERC
Paul Terrien
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • 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
    • F25J3/0209—Natural gas or substitute natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • 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
    • F25J3/0266—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 dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • 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
    • B01D53/22—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 diffusion
    • 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • 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
    • 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
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • 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
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation 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
    • F25J2210/04—Mixing or blending of fluids with the feed 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust 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
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • 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
    • F25J2230/32—Compression of the product 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being carbon dioxide
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • 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
    • 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

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

In a process for separating a feed stream (1) comprising at least C02 and also at least one light compound, a C02-rich product (9) and a C02-depleted gas (11) are produced via a process of partial condensation and optionally of distillation using at least one first phase separation pot (7, 10, 22), C02-depleted gas is introduced into a C02-selective separation process (15) in order to obtain a first fluid (19) whose C02 concentration is higher than that of the feed stream and a fluid (17) enriched in at least one of the light compounds, and a second C02-rich product (27) and a second C02 depleted gas (25) are produced from the C02-charged first fluid, using a second phase separation pot (23) different from the first phase separation pot. /31 17 1 155 23 19 213 3 C02 2 [Fig. 1] 29 31 17 1 25 23 19 21 r3 C02 2 27 1/ 7 9 1/4

Description

[Fig. 1]
29 31
17 1
25 23 19 21 r3 C02 2 27 7 1/
9
1/4
DESCRIPTION Title: Process and apparatus for separating a feed stream comprising at least C02 and also at least one light compound
This application claims priority from French application number 1873355 filed on 19 December 2018, the contents of which are to be taken as incorporated herein by this reference. The present invention relates to a process and apparatus for separating a feed stream comprising at least C02 and also at least one light compound. As a result of global warming, the increasing demand for gas for EOR or the need to purify the acidic gas from natural gas, C02 separation is increasingly employed. Cryogenic separation solutions coupled with membranes notably allow very high C02 uptake yields, of up to 99%. In these schemes, the gases to be freed of C02 are mixed with the membrane permeates at relatively low pressure, compressed and then cooled and partially condensed. The liquid part forms the C02 production. The gas part is sent to the membranes. These two parts are separated in a phase separator. The membrane residue consists of the C02-freed gas. EP2685190A1 presents an example of such a process with the particular feature of using the membrane permeate to perform an additional step of regeneration of the dryers. The advantage of this scheme is the mutualization of the compression function of the gas to be purified and of the membrane permeate in the same compressor. Significant cost savings are thus made. As the purity of the permeate is often quite similar to that of the gas to be purified, the two gases can be mixed without significant loss of separation energy. As regards the generation of cold to ensure the cooling of the mixture of the gas to be purified and of the permeate, at least a portion of the liquid derived from the condensation is usually expanded at several pressure levels and then vaporized and heated against this mixture. As regards the various pressure levels: • A portion of the liquid is usually expanded at a pressure close to that of the triple point of C02, making it possible to generate a fluid at the lowest temperature without forming a solid. The corresponding pressure is between 5.1 and 7 bara.
• The temperature required to form the first drop of C02 during the condensation of the mixture of gas to be purified and permeate is proportionately lower the more the mixture is depleted in C02. As a result, it is necessary to expand the liquid obtained at pressures that are proportionately lower to generate cold fluids at temperatures that are proportionately lower.
[Fig 4] shows on the x-axis the temperature in °C and the heat transfer in kcal/hour on the y-axis. As may be seen, the majority of the refrigeration must be generated at temperatures below -25C. Furthermore, in this case, the curves are very much separated at the hot end (difference of more than 100 C), which means that it is not necessary to generate a very large amount of cold to ensure cooling at the lowest temperatures. • The heated gases obtained are usually compressed in order to enable transportation of the C02. In this case, the same compressor is usually used for the various gas streams. Thus, the various pressure levels must be compatible with the intermediate pressures of the compressor. This will thus give the second pressure level between 8 and 14 bara. A third compression level is not envisageable since the cold generated for this level would be at too high a temperature (see the preceding point). However, in certain cases, the C02 purity of the permeate is markedly higher than that of the gas to be purified. This is the case in particular when the gas to be purified has C02 contents below 50 mol%. Thus, by mixing the permeate with the gas to be purified, the permeate is diluted. A significant portion of the separation that has been achieved is lost due to this dilution. This case arises notably for the separation of C02 from natural gas where the membrane permeate may contain up to 90 mol% of C02 whereas the acidic natural gas to be purified may contain only 30 mol% of C02. Furthermore, a certain number of compounds may also be separated in the membranes and evacuated in the residue. Mixing the permeate of the membranes that are depleted in these compounds with the gas to be purified which contains same does not make it possible to fully exploit the separation performed in the membranes. This case also arises for the separation of C02 from natural gas where the hydrocarbons cross the membrane very little. The permeate predominantly containing C02 and CH4 is thus significantly depleted in C2+. Mixing it with the gas to be purified which contains a larger amount thereof does not make it possible to exploit this separation.
The present invention allows the energy optimization of process schemes employing cryogenic separation and membranes. It consists in not mixing the membrane permeate with the gas to be purified and in cooling and partially condensing it in a dedicated separating pot. According to one subject of the invention, a process is provided for separating a feed stream comprising at least C02 and at least one light compound chosen from CH4, CO, H2, N2, 02, Ar, C2+ comprising at least the following steps: a) Production of a C02-rich product and of a C02-depleted gas via a process of at least one partial condensation of the feed stream using at least one first phase separation pot, b) Introduction of the C02-depleted gas into a C02-selective permeation process in order to obtain as permeate a first fluid whose C02 concentration is greater than that of the feed stream and as non-permeate a fluid enriched in at least one of the light compounds and c) Production of a second C02-rich product and of a second C02-depleted gas from the first C02-charged fluid obtained in b) or from a fluid derived therefrom via a process of partial condensation and optionally distillation, using a second phase separation pot different from the first phase separation pot, without having mixed the first fluid with the feed stream. According to other optional aspects: • the first fluid contains at least 70 mol% of C02. • the feed stream contains not more than 50 mol% of C02 and the C02 selective separation process is a permeation and/or adsorption process. • the stream contains C2+ and the fluid enriched in light compound is enriched in C2+. • the second C02-depleted gas is mixed with the C02-depleted gas sent into the permeation process • the second C02-depleted gas feeds the distillation column • at least during step a), the process comprises distillation in a distillation column Sa portion of the first fluid is injected in gaseous form into the distillation column tank. • the portion of the first fluid is a fluid coming from a compression step downstream of the selective separation process.
• at least during step a), the process comprises distillation in a distillation column and at least a portion of the second product feeds the distillation column. • at least a portion of the product feeds the distillation column • step a) comprises partial condensation in a shell-and-tube heat exchanger. According to another aspect of the invention, apparatus is provided for separating a feed stream comprising at least C02 and at least one light compound chosen from CH4, CO, H2, N2, 02, Ar, C2+ comprising at least: a) Partial condensation apparatus comprising at least one first phase separation pot for producing a C02-rich product and a C02-depleted gas, b) C02-selective permeation apparatus fed with C02-depleted gas in order to obtain a permeate which is a first fluid whose C02 concentration is greater than that of the feed stream and a non-permeate which is a fluid enriched in at least one of the light compounds and c) Apparatus for partial condensation and optionally distillation, comprising a second phase separation pot different from the first phase separation pot fed with permeate without needing to be mixed with the feed stream to produce a second C02 rich product and a second C02-depleted gas from the first C02-charged fluid obtained in b). The apparatus may comprise a distillation column and means for delivering the C02-depleted second gas thereto. The apparatus may comprise: • a distillation column and means for delivering at least one C02-rich product thereto. • means for delivering the C02-rich product and the second C02-rich product to the distillation column. • means for expanding the two products together upstream of the distillation column. • means for expanding the two products separately upstream of the distillation column. This solution has a certain number of advantages: • Since the permeate is more charged with C02, its condensation begins at a higher temperature. This makes it possible to generate a portion of the refrigeration at higher temperature and thus at higher pressure. Thus, a portion of the liquid C02 can be expanded at a higher pressure, allowing a saving in recompression energy.
• [Fig 5] shows on the x-axis the temperature in °C and the heat transfer in kcal/h on the y-axis, which is visualized by means of the corresponding diagram. Relative to Figure 4, it is seen that an additional vaporization stage has been added at about -15 0 C (-21 bara). • In the particular case of separating C02 from natural gas, the membrane permeate is sparingly charged with C2+ hydrocarbons. In the case where these hydrocarbons are to be separated out, in particular in the case of separating out the C2 as described in WO 2016/156691, the liquid coming from the partial condensation of the membrane permeate requires less substantial stripping than the rest of the liquid obtained by partial condensation of the feed gas. It is thus not necessary to expend energy to distil this gas for the purpose of separating out the ethane. There is thus also an energy saving. Furthermore, since the gas resulting from the stripping is recycled into the permeate compression machine, reducing its flow rate allows savings on the size of the machine and on the number of modules required. • In the particular case of separating C02 from natural gas, since the natural gas is already available at high pressure, a compressor for the membrane permeate is necessary. Thus, whether the permeate is mixed with the gas to be purified as in the prior art or condensed separately according to the invention, this does not require an additional machine. Preferably, the selective permeation process is performed at a temperature of between -30 0C and 100 0C. It may nevertheless be performed at a temperature below -30 0C or between 30 0C and 90 0C. The working pressure is between 1.5 bara and 90 bara. The invention will be described in greater detail with reference to the figures, which show processes for separating a mixture containing carbon dioxide and a lighter compound according to the invention.
[Fig 1] represents a process for separating a feed stream comprising at least C02 according to the invention.
[Fig 2] represents a process for separating a feed stream comprising at least C02 according to the invention.
[Fig 3] represents a process for separating a feed stream comprising at least C02 according to the invention. In the process of Figure 1, a feed stream 1 comprising at least C02, optionally less than 50 mol% of C02 and also a light compound chosen from CH4, CO, H2, N2,
02, Ar. The stream may also contain hydrocarbons C2+. This stream may, for example, be natural gas, available at high pressure, for example about 50 bara. The stream 1 is optionally compressed with a compressor 3 and is cooled in a shell and tube heat exchanger 5 to a temperature below -200 C where it becomes partially condensed. The partially condensed flow is delivered to a phase separator 7 working at a temperature below 0°C. The liquid 9 produced by the phase separator 7 constitutes a carbon dioxide-rich product, optionally containing at least 70 mol% of C02, or even at least 90 mol% of C02. The gas 11 from the phase separator heats up in the heat exchanger, after having been mixed with a flow 25 to form a flow 13. The flow 13 heated in the exchanger 5 is delivered to a process 15 for producing a gaseous permeate 19 that is enriched in carbon dioxide relative to the gas 13 and preferably relative to the gas 1. The gas 19 may also be significantly depleted in C2+ if the gas 1 contains any. The process enabling this enrichment and optionally this depletion is a permeation process, for example a membrane permeation process. Process 15 also produces a gaseous non-permeate 17 that is depleted in C02 and enriched in at least one light compound. The gas 17 may be enriched in at least one component chosen from the group CH4, CO, H2, N2, 02, Ar, C2+. The gas 19 is cooled in the exchanger 6 after compression with a compressor 21. It is partially condensed in the exchanger 6 and separated in a second phase separator 23 which produces a carbon dioxide-enriched liquid product 27. It also produces a carbon dioxide-depleted flow 25 which is mixed with the flow 11 as described above. Thus, the gas 19 which constitutes here the membrane permeate is not mixed with the gas 1 to be purified, but is cooled and partially condensed in a dedicated separating pot 23. The cold for the process is at least partly provided by a cold source 29 which delivers a refrigerant fluid 31 to the exchanger 5. The process of Figure 2 uses a process of partial condensation followed by distillation to separate the feed stream 1. The process comprises a single distillation column (no first column, the main objective of which is to strip out the C2+) but uses an intermediate condensation pressure.
The stream 1 comprises at least C02, optionally less than 50 mol% of C02 and also at least one light compound chosen from CH4, CO, H2, N2, 02, Ar. The stream may also contain hydrocarbons C2+. In this variant, the stream 1 is wet. It passes into a valve 2, in two systems 4,6 to remove the water and is then cooled in a shell and tube heat exchanger 5 where it partially condenses. The partially condensed flow is delivered to a phase separator 22 working at a temperature below °C. The liquid 202 produced by the phase separator 22 constitutes a carbon dioxide rich product, optionally containing at least 70 mol% of C02, or even at least 90 mol% of C02. The gas 201 from the phase separator 22 is partially condensed in the shell and tube exchanger 10. The two-phase fluid is separated in a second phase separator 7. The liquids 202,9 from the first phase separator 22 and from the second phase separator 7 are mixed, expanded with a valve 203 and delivered as the flow 204 to a distillation column 206. The distillation column tank liquid 207 is a flow constituting a C02-rich product. The flow 207 is expanded with a valve 208 and delivered to the exchanger 10 where it partially vaporizes. The gas formed 209 is heated in the exchanger 6, compressed with a compressor 210 and constitutes a portion of the C02-rich product 211. The rest of the product 211 is produced by pressurizing the liquid 213 from the exchanger 10 with a pump 215 to form a pressurized liquid 219 which passes into a valve 220 and is then vaporized in the exchanger 6 to form a flow to be mixed with the flow 209. The head gas 221 from the distillation column 206 is heated in the heat exchanger 6, compressed with the compressor 223 and joins the flow 1 upstream of the heat exchanger6. The gas 11 from the second phase separator 7 is heated in the phase separator and is then separated by a process 15 for producing a gaseous permeate 19 that is enriched in carbon dioxide relative to the gas 13 and preferably relative to the gas 1. The gas 19 may also be significantly depleted in C2+ if the gas 1 contains any. The process enabling this enrichment and optionally this depletion is a permeation process, for example a membrane permeation process. Process 15 also produces a gaseous non-permeate 17 that is depleted in C02 and enriched in at least one light compound. The gas 17 may be enriched in at least one component chosen from the group CH4, CO, H2, N2, 02, Ar, C2+. The gas 19 is cooled in the exchanger 6 after compression with a compressor 21A,21B,21C. It is partially condensed in the exchanger 6 and separated in a second phase separator 23 which produces a carbon dioxide-enriched liquid 27. It also produces a carbon dioxide-depleted flow 25 which is mixed with the gas 221 coming from the distillation column. The carbon dioxide-enriched liquid 27 is expanded with the valve 28 and delivered to the distillation column 206 as feed stream. Thus, the gas 19 which constitutes here the membrane permeate is not mixed with the gas 1 to be purified, but is cooled and partially condensed in a dedicated separating pot 23. The process of Figure 2 uses a process of partial condensation followed by distillation to separate the feed stream 1. The process comprises a single distillation column (no first column, the main objective of which is to strip out the C2+) but uses an intermediate condensation pressure. The stream 1 comprises at least C02, optionally less than 50 mol% of C02 and also at least one light compound chosen from CH4, CO, H2, N2, 02, Ar. The stream may also contain hydrocarbons C2+. In this variant, the stream 1 is wet. It passes into a valve 2, in two systems 4,6 to remove the water and is then cooled in a shell and tube heat exchanger 5 where it partially condenses. The partially condensed flow is delivered to a phase separator 22 working at a temperature below °C. The liquid 202 produced by the phase separator 22 constitutes a carbon dioxide rich product, optionally containing at least 70 mol% of C02, or even at least 90 mol% of C02. The gas 201 from the phase separator 22 is partially condensed in the shell and tube exchanger 10. The two-phase fluid is separated in a second phase separator 7. The liquids 202,9 from the first phase separator 22 and from the second phase separator 22 are mixed, expanded with a valve 203 and delivered as the flow 204 to a distillation column 206. The distillation column tank liquid 207 is a flow constituting a C02-rich product. The flow 207 is expanded with a valve 208 and delivered to the exchanger 10 where it partially vaporizes. The gas formed 209 is heated in the exchanger 6, compressed with a compressor 210 and constitutes a portion of the C02-rich product 211. The rest of the product 211 is produced by pressurizing the liquid 213 from the exchanger 10 with a pump 215 to form a pressurized liquid 219 which passes into a valve 220 and is then vaporized in the exchanger 6 to form a flow to be mixed with the flow 209. Optionally, a portion of the first fluid 19 compressed in the compressors 21A, 21B, 21C may be delivered to the column tank to be separated therein (illustrated in dotted lines).
The head gas 221 from the distillation column 206 is heated in the heat exchanger 6, compressed with the compressor 223 and joins the flow 1 upstream of the heat exchanger6. The gas 11 from the second phase separator 7 is heated in the phase separator and is then separated by a process 15 for producing a gas 19 that is enriched in carbon dioxide relative to the gas 13 and preferably relative to the gas 1. The gaseous permeate 19 may also be significantly depleted in C2+ if the gas 1 contains any. The process enabling this enrichment and optionally this depletion is a permeation process, for example a membrane permeation process. Process 15 also produces a gaseous non-permeate 17 that is depleted in C02 and enriched in at least one light compound. The gas 17 may be enriched in at least one component chosen from the group CH4, CO, H2, N2, 02, Ar, C2+. The gas 19 is cooled in the exchanger 6 after compression with a compressor 21A,21B,21C. It is partially condensed in the exchanger 6 and separated in a second phase separator 23 which produces a carbon dioxide-enriched liquid 27. It also produces a carbon dioxide-depleted flow 25 which is mixed with the gas 221 coming from the distillation column. The carbon dioxide-enriched liquid 27 is expanded with the valve 28 and delivered to the distillation column 206 as feed stream. Thus, the gas 19 which constitutes here the membrane permeate is not mixed with the gas 1 to be purified, but is cooled and partially condensed in a dedicated separating pot 23. A portion 217 of the pumped liquid 213 is expanded and vaporized in the exchanger 5. It is then delivered to the distillation column tank 206 without having been cooled in the heat exchanger 5, to provide reboiling heat. It is the vaporization of this liquid 213 which will provide the additional vaporization stage at about -15°C (-25 bara). The process of Figure 3 uses a process of partial condensation followed by distillation to separate the feed stream 1. The process differs from that of Figure 2 in that it comprises a C2+ stripping step. As in Figure 2, it uses an intermediate condensation pressure. The stream 1 comprises at least C02, optionally less than 50 mol% of C02 and also at least one light compound chosen from CH4, CO, H2, N2, 02, Ar. The stream may also contain hydrocarbons C2+. In this variant, the stream 1 is wet. It passes into a valve 2, in two systems 4,6 to remove the water and is then cooled in a shell and tube heat exchanger 5 where it partially condenses. The partially condensed flow is delivered to a phase separator 22 working at a temperature below °C. The liquid 202 produced by the phase separator 22 constitutes a carbon dioxide rich product, optionally containing at least 70 mol% of C02, or even at least 90 mol% of C02. The gas 201 from the phase separator 22 is partially condensed in the shell and tube exchanger 10. The two-phase fluid is separated in a second phase separator 7. The liquids 202,9 from the first phase separator 22 and from the second phase separator 22 are mixed, expanded with a valve 203 and delivered as the flow 204 to a distillation column 206. The distillation column tank liquid 207 is a flow constituting a C02-rich product. The flow 207 is expanded with a valve 208 and delivered to the exchanger 10 where it partially vaporizes. The gas formed 209 is heated in the exchanger 6, compressed with a compressor 210 and constitutes a portion of the C02-rich product 211. The rest of the product 211 is produced by pressurizing the liquid 213 from the exchanger 10 with a pump 215 to form a pressurized liquid 219 which passes into a valve 220 and is then vaporized in the exchanger 6 to form a flow to be mixed with the flow 209. The head gas 221 from the distillation column 206 is heated in the heat exchanger 6, compressed with the compressor 223 and joins the flow 1 upstream of the heat exchanger6. The gas 11 from the second phase separator 7 is heated in the phase separator and is then separated by a process 15 for producing a gas 19 that is enriched in carbon dioxide relative to the gas 13 and preferably relative to the gas 1. The gas 19 may also be significantly depleted in C2+ if the gas 1 contains any. The process enabling this enrichment and optionally this depletion may be a permeation process, for example a membrane permeation process, and/or an adsorption process, for example TSA, PSA, VSA. Process 15 also produces a gas 17 that is depleted in C02 and enriched in at least one light component. The gas 17 may be enriched in at least one component chosen from the group CH4, CO, H2, N2, 02, Ar, C2+. The gas 19 is cooled in the exchanger 6 after compression with a compressor 21A,21B,21C. It is partially condensed in the exchanger 6 and separated in a second phase separator 23 which produces a carbon dioxide-enriched liquid 27. It also produces a carbon dioxide-depleted flow 25. The carbon dioxide-enriched liquid 27 is expanded with the valve 28 and delivered to the distillation column 206 as feed stream. Thus, the gas 19 which constitutes here the membrane permeate is not mixed with the gas 1 to be purified, but is cooled and partially condensed in a dedicated separating pot 23. Optionally, a portion 217 of the pumped liquid 213 may be expanded and vaporized in the exchanger 5. It is then delivered to the distillation column tank 206 without having been cooled in the heat exchanger 5, to provide reboiling heat. The carbon dioxide-depleted flow 25 is mixed with the gas 217 and also serves for the reboiling of the column 206. Optionally, a portion of the first fluid 19 compressed in the compressors 21A,21B,21C may be delivered to the column tank to be separated therein (illustrated in dotted lines). The discussion of documents, acts, materials, devices, articles and the like is included in this specification solely for the purpose of providing a context for the present invention. It is not suggested or represented that any or all of these matters formed part of the prior art base or were common general knowledge in the field relevant to the present invention as it existed before the priority date of each claim of this application. Where the terms "comprise", "comprises", "comprised" or "comprising" are used in this specification (including the claims) they are to be interpreted as specifying the presence of the stated features, integers, steps or components, but not precluding the presence of one or more other features, integers, steps or components, or group thereof.

Claims (15)

THE CLAIMS DEFINING THE INVENTION ARE AS FOLLOWS:
1. Process for separating a feed stream comprising at least C02 and also at least one light compound chosen from CH4, CO, H2, N2, 02, Ar, C2+ comprising at least the following steps: a) Production of a C02-rich product and of a C02-depleted gas via a process of at least one partial condensation of the feed stream using at least one first phase separation pot, b) Introduction of the C02-depleted gas into a C2-selective permeation process in order to obtain as permeate a first fluid whose C02 concentration is greater than that of the feed stream and as non-permeate a fluid enriched in at least one of the light compounds and c) Production of a second C02-rich product and of a second C02-depleted gas from the first C02-charged fluid obtained in b) or from a fluid derived therefrom via a process of partial condensation and optionally distillation, using a second phase separation pot different from the first phase separation pot, without having mixed the first fluid with the feed stream.
2. Process according to Claim 1, in which the feed stream contains not more than 50 mol% of C02 and the first fluid contains at least 70 mol% of C02.
3. Process according to Claim 1 or Claim 2, in which the second C02-depleted gas is mixed with the C02-depleted gas sent into the permeation process.
4. Process according to any one of the preceding claims, in which the stream contains C2+ and the fluid enriched in light compound is enriched in C2+.
5. Process according to any one of the preceding claims, in which: • at least during step a), the process comprises distillation in a distillation column Sa portion of the first fluid is injected in gaseous form into the distillation column tank.
6. Process according to Claim 6, in which the portion of the first fluid is a fluid coming from a compression step downstream of the selective permeation process.
7. Process according to any one of the preceding claims, in which, at least during step a), the process comprises distillation in a distillation column and at least a portion of the second product feeds the distillation column.
8. Process according to Claim 7, in which at least a portion of the product feeds the distillation column.
9. Process according to any one of the preceding claims, in which step a) comprises partial condensation in a shell-and-tube heat exchanger.
10. Apparatus for separating a feed stream comprising at least C02 and also at least one light compound chosen from CH4, CO, H2, N2, 02, Ar, C2+ comprising at least: a) Apparatus for partial condensation and optionally distillation, comprising at least one first phase separation pot for producing a C02-rich product and a C02 depleted gas, b) C02-selective permeation apparatus fed with C02-depleted gas in order to obtain a permeate which is a first fluid whose C02 concentration is greater than that of the feed stream and a non-permeate which is a fluid enriched in at least one of the light compounds and c) Partial condensation apparatus, comprising a second phase separation pot different from the first phase separation pot fed with permeate without having mixed it with the feed stream to produce a second C02-rich product and a second C02-depleted gas from the first C02-charged fluid obtained in b).
11. Apparatus comprising a distillation column and means for delivering the C02 depleted second gas thereto.
12. Apparatus comprising a distillation column and means for delivering at least one C02-rich product thereto.
13. Apparatus according to Claim 12, comprising means for delivering the C02 rich product and the second C02-rich product to the distillation column.
14. Apparatus according to Claim 13, comprising means for expanding the two products together upstream of the distillation column
.
15. Apparatus according to Claim 13, comprising means for expanding the two products separately upstream of the distillation column.
[Fig. 1]
1/4
[Fig. 2]
2/4
[Fig. 3]
3/4
[Fig. 5]
[Fig. 4]
4/4
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