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US20110252827A1 - CO2 Recovery And Cold Water Production Method - Google Patents

CO2 Recovery And Cold Water Production Method Download PDF

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Publication number
US20110252827A1
US20110252827A1 US13/133,448 US200913133448A US2011252827A1 US 20110252827 A1 US20110252827 A1 US 20110252827A1 US 200913133448 A US200913133448 A US 200913133448A US 2011252827 A1 US2011252827 A1 US 2011252827A1
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Prior art keywords
fluid
solid
gas
process fluid
cooling
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Abandoned
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US13/133,448
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English (en)
Inventor
Frederick Lockwood
Jean-Pierre Tranier
Claire Weber
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Assigned to L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: LOCKWOOD, FREDERICK, RAVEX, ALAIN, TRANIER, JEAN-PIERRE, WEBER, CLAIRE
Publication of US20110252827A1 publication Critical patent/US20110252827A1/en
Abandoned legal-status Critical Current

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    • 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
    • B01D53/002—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 condensation
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15061—Deep cooling or freezing of flue gas rich of CO2 to deliver CO2-free emissions, or to deliver liquid CO2
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
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    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/14—Coke-ovens gas
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    • 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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2220/84—Separating high boiling, i.e. less volatile components, e.g. NOx, SOx, H2S
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2230/30—Compression of the feed stream
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/58—Quasi-closed internal or closed external argon refrigeration cycle
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
    • 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

Definitions

  • the present invention relates to a method of capturing carbon dioxide in a fluid comprising at least one compound more volatile than carbon dioxide CO2, for example methane CH4, oxygen O2, argon Ar, nitrogen N2, carbon monoxide CO, helium He and/or hydrogen H2.
  • the invention can be notably applied to units producing electricity and/or steam from carbon fuels such as coal, hydrocarbons (natural gas, fuel oil, petrochemical residue, etc), household waste, biomass but can also be applied to gases from refineries, chemical plants, steel-making plants or cement works, to the treatment of natural gas as it leaves production wells. It could also be applied to the flue gases from boilers used to heat buildings or even to the exhaust gases from transport vehicles, and more generally to any industrial process that generates CO2-containing flue gases.
  • carbon fuels such as coal, hydrocarbons (natural gas, fuel oil, petrochemical residue, etc), household waste, biomass
  • gases from refineries, chemical plants, steel-making plants or cement works, to the treatment of natural gas as it leaves production wells. It could also be applied to the flue gases from boilers used to heat buildings or even to the exhaust gases from transport vehicles, and more generally to any industrial process that generates CO2-containing flue gases.
  • Carbon dioxide is a greenhouse gas.
  • it is becoming increasingly desirable to reduce or even eliminate discharges of CO2 into the atmosphere by capturing it and then, for example, storing it in appropriate geological layers or by realizing it as an asset in its own right.
  • Document FR-A-2894838 discloses the same type of method, with some of the liquid CO2 produced recirculated.
  • the cold may be supplied by vaporizing LNG (liquefied natural gas). This synergy reduces the specific energy consumption of the method, although this remains high despite this, and requires an LNG terminal.
  • LNG liquefied natural gas
  • the invention relates first of all to a method for producing chilled water, at least one CO2-lean gas and one or more CO2-rich primary fluids from a process fluid containing CO2 and at least one compound more volatile than CO2 and industrial water, comprising the following steps:
  • the process fluid generally comes from a boiler or any plant that produces flue gases. These flue gases may have undergone various pre-treatments, notably with a view to removing NOx (oxides of nitrogen), dust, SOx (oxides of sulfur) and/or water.
  • NOx oxides of nitrogen
  • SOx oxides of sulfur
  • the process fluid Prior to separation, the process fluid is either monophasic, in gaseous or liquid form, or polyphasic.
  • gaseous form is “essentially gaseous” form, that is to say that it may notably contain dust, solid particles such as soot and/or droplets of liquid.
  • the process fluid contains CO2 that is to be separated from the other constituents of said fluid by cryo-condensation.
  • These other constituents comprise one or more compounds more volatile than carbon dioxide in terms of condensation, for example methane CH4, oxygen O2, argon Ar, nitrogen N2, carbon monoxide CO, helium He and/or hydrogen H2.
  • the process fluids generally comprise predominantly nitrogen or predominantly CO or predominantly hydrogen.
  • step a) the process fluid is separated into at least one CO2-lean gas and one or more CO2-rich primary fluids using methods known to those skilled in the art.
  • this may be a separation method using low-temperature solid cryo-condensation of the CO2.
  • step b) the CO2-lean gas produced in step a) is brought into direct contact with one or more streams of industrial water. This contact between a gas that is not saturated with water and water causes some of said industrial water to vaporize. The heat of vaporization of this water and any possible heating-up of the CO2-lean gas serves to cool the non-vaporized water.
  • a direct-contact tower may simply consist of a spray system so as to form water droplets which, under the action of gravity, will drop down against the flow of the CO2-lean gas.
  • use may also be made of gas-liquid contactors of the plates or packings (loose or structured) type.
  • the method according to the invention may comprise one or more of the following features:
  • step a1) the process fluid is first of all cooled without a change in state.
  • This cooling may advantageously take place at least in part by exchange of heat with CO2-rich fluids from the separation process.
  • it may advantageously take place at least in part by exchange of heat with the CO2-lean gas from the separation process.
  • Step a2) consists in solidifying the initially gaseous CO2 by raising the process fluid to a temperature below the triple point for CO2 while the partial pressure of the CO2 in the process fluid is below that of the triple point for CO2. For example, the total pressure of the process fluid is close to atmospheric pressure.
  • This solidification operation is sometimes known as “cryo-condensation” or “anti-sublimation” of the CO2 and, by extension, of the process fluid.
  • CO2-lean gas that is to say will constitute said gas that comprises less than 50% CO2 by volume and preferably less than 10% CO2 by volume.
  • said CO2-lean gas contains less than 1% CO2 by volume.
  • it contains more than 2% thereof.
  • it contains more than 5% thereof.
  • This solid may comprise other compounds than CO2. Mention may, for example, be made of other compounds which might also have solidified, or alternatively of bubbles and/or drops of fluid contained within said solid lump. This explains how the solid could potentially consist of not only solid CO2. This “solid” may contain non-solid parts such as fluid inclusions (drops, bubbles, etc).
  • This solid is then isolated from the compounds that have not solidified after cryo-condensation and recovered.
  • step a3) it is returned to temperature and pressure conditions such that it changes into a fluid, liquid and/or gaseous, state. At least part of said solid may then liquefy. This then gives rise to one or more CO2-rich primary fluids. These fluids are said to be “primary” to distinguish them from treatment fluids which are said to be “secondary”. What is meant by “CO2-rich” is something “comprising predominantly CO2” within the meaning defined hereinabove.
  • the inventors have demonstrated that it is particularly advantageous to carry out the first and/or the second cooling of the process fluid using one or more refrigerating cycles each comprising at least one near-isentropic expansion of a gas.
  • These refrigerating cycles consist of several steps which cause a so-called “working” fluid to pass via several physical states characterized by given composition, temperature, pressure, etc conditions.
  • the presence, among the steps of the cycle, of at least one near-isentropic expansion that is to say of an expansion that causes the entropy of the expanded fluid to increase by less than 25%, preferably less than 15% and more preferably still, less than 10% makes it possible to improve the energy consumption of the separation process.
  • some of the near-isentropic expansions of the refrigerating cycle or cycles provide work. They are, for example, carried out by introducing working fluid into a turbine.
  • the working fluids may be of varying kinds. According to various embodiments, these fluids may comprise nitrogen and/or argon. They may also comprise all or part of the CO2-lean gas obtained or of the process fluid. These fluids may be mixed with other fluids or have undergone intermediate steps of compression, expansion, etc.
  • the near-isentropic expansion or expansions that do not provide external work may give rise to a cooling of the working fluid such that solid CO2 appears. This may constitute all or part of the second cooling of the process fluid.
  • these near-isentropic expansions are carried out through a Venturi (a throat with Venturi effect).
  • the abovementioned causing of the fluid to rotate can be obtained by any conventional means, for example by suitably oriented vanes.
  • the increase in speed is achieved through a Venturi effect.
  • the temperature of the working fluid drops. Solid particles of CO2 appear.
  • the fluid has a rotational movement about an axis substantially parallel to the direction of the flow, like a corkscrew. This creates a centrifugal effect allowing these solid particles to be recovered at the periphery of the flow.
  • any work that might be produced by the near-isentropic expansion or expansions serves in part to compress the fluids in other steps of the method.
  • the invention also relates to the method applied to industrial flue gases with a view to capturing CO2.
  • these flue gases come from a plant producing energy (steam, electricity) and may have undergone pretreatments.
  • FIG. 1 schematically depicts a plant employing a method according to the invention, with a refrigerating cycle employing an auxiliary fluid as working fluid,
  • FIG. 13 schematically depicts a plant employing a method according to the invention with, on the one hand, a cycle for producing energy using the cold of fusion of solid CO2 and, on the other hand, additional purifications by distillation of the compounds less volatile than CO2, then the compounds more volatile than CO2,
  • FIGS. 2 to 7 schematically depict alternative forms of refrigerating cycles that can be associated with the invention:
  • FIG. 2 schematically depicts an alternative form, with a refrigerating cycle using the CO2-lean gas by way of working fluid and comprising a near-isentropic expansion with the production of work
  • FIG. 3 schematically depicts an alternative form, with a refrigerating cycle using the CO2-lean gas as working fluid and comprising a near-isentropic expansion with the production of work
  • FIG. 4 schematically depicts an alternative form of the method with a refrigerating cycle using the process fluid as working fluid and comprising a near-isentropic expansion with the production of work, during which there is no cryo-condensation of CO2,
  • FIG. 5 schematically depicts an alternative form with a refrigerating cycle using the process fluid as working fluid and comprising a near-isentropic expansion with the production of work, during which there is cryo-condensation of CO2,
  • FIG. 6 schematically depicts part of an alternative form with a refrigerating cycle using the process fluid as working fluid and comprising a near-isentropic expansion without the production of work, during which there is cryo-condensation of CO2,
  • FIG. 7 schematically depicts an alternative form, in which the second cooling also comprises liquefaction and further comprising a refrigerating cycle using the process fluid as working fluid and comprising near-isentropic expansions without the production of work during which expansions there is cryo-condensation of CO2,
  • FIG. 8 schematically depicts the use of a method according to the invention in a plant for producing electricity on the basis of coal with combustion in air
  • FIG. 9 schematically depicts the use of a method according to the invention in a plant for producing electricity on the basis of coal with hybrid combustion or combustion in oxygen,
  • FIG. 10 schematically depicts a method of separating a gas from a steel-making plant to obtain a CO2-lean gas 927 and a CO2-rich primary fluid 73 ; the invention could in this case be applied by bringing the dry CO2-lean gas 927 into direct contact with the industrial water so as to obtain chilled water (not depicted) for use in the exchangers 906 and/or 105 .
  • FIG. 11 schematically depicts a method of separating a synthesis gas from a synthesis gas production plant operating on oxygen; the invention could in this case be applied by bringing the dry CO2-lean gas 927 into direct contact with the industrial water so as to obtain chilled water (not depicted) for use in an exchanger of the unit 907 and/or in the exchanger 105 .
  • FIG. 12 schematically depicts a method for separating a synthesis gas from a plant for producing carbon monoxide from a synthesis gas that comes from a steam reforming of a synthesis gas; the invention could in this case be applied by bringing a CO2-lean gas 927 and/or a dry gas 929 into direct contact with the industrial water so as to obtain chilled water (not depicted) for use in the exchangers 906 and/or 105 .
  • FIGS. 14 and 15 depict a turbine for carrying out a near-isentropic expansion of the process fluid with the production of external work.
  • the plant illustrated in FIG. 1 implements the steps described below.
  • the fluid 24 consisting of flue gases is compressed in a compressor 101 , notably to compensate for the pressure losses in the various pieces of equipment in the plant.
  • this compression may also be combined with the compression known as the draft compression of the boiler that produces the flue gases. It may also be carried out between other steps of the method, or downstream of the CO2 separation method;
  • the compressed fluid 30 is injected into a filter 103 to eliminate particles down to a level of concentration of below 1 mg/m 3 , preferably of below 100 ⁇ g/m 3 .
  • the dust-free fluid 32 is cooled to a temperature close to 0° C., generally of between 0° C. and 10° C., so as to condense the water vapor it contains.
  • This cooling is carried out in a tower 105 , with water injected at two levels, the cold water 36 and water 34 at a temperature close to the wet-bulb temperature of the ambient air. It is also possible to conceive of indirect contact.
  • the tower 105 may or may not have packings.
  • the fluid 38 is sent to a unit that eliminates residual water vapor 107 , for example using one and/or another of the following methods:
  • the dried fluid 40 is then introduced into the exchanger 109 where the fluid is cooled down to a temperature close to, but in all events higher than, the temperature at which CO2 solidifies.
  • This temperature can be determined by a person skilled in the art aware of the pressure and composition of the process fluid 40 . This temperature is situated at around about ⁇ 100° C. if the CO2 content of the process fluid is of the order of 15% by volume and for a pressure close to atmospheric pressure.
  • the fluid 42 which has undergone a first cooling 109 is then introduced into a vessel 111 where it continues to be cooled down to the temperature that provides the desired level of CO2 capture. Cryo-condensation of at least part of the CO2 contained in the fluid 42 occurs producing, on the one hand, a CO2-lean gas 44 and, on the other hand, a solid 62 comprising predominantly CO2.
  • the gas 44 leaves the vessel 111 at a temperature of the order of ⁇ 120° C. This temperature is chosen as a function of the target level of CO2 capture. At this temperature, the CO2 content of the gas 44 is of the order of 1.5% by volume, namely a capture level of 90% starting out from a process fluid containing 15% CO2.
  • the fluid 46 is then heated up in the exchanger 109 .
  • the fluid 48 can also be used notably to regenerate the unit used for eliminating residual vapor 107 and/or for producing cold water 36 a by evaporation in a direct-contact tower 115 into which a dry fluid 50 is introduced which then becomes saturated with water, vaporizing some of it.
  • the cold water could then potentially undergo additional cooling in a refrigerator unit 119 .
  • the solid 62 comprising predominantly CO2 is transferred to a bath 121 of liquid CO2.
  • This bath 121 needs to be heated in order to remain liquid, to compensate for the addition of cold from the solid 62 (latent heat of fusion and sensible heat). This can be done in various ways:
  • Liquid 64 comprising predominantly CO2 is tapped from the bath 121 .
  • This liquid is split into three streams.
  • the first is obtained by an expansion 65 to 5.5 bar absolute producing a diphasic, gas-liquid, fluid 66 .
  • the second, 68 is obtained by compression 67 , for example to 10 bar.
  • the third, 70 is compressed for example to 55 bar.
  • the 5.5 bar level provides cold at a temperature close to the triple point temperature for CO2.
  • the 10 bar level allows the transfer of the latent heat of vaporization of the fluid 68 at around ⁇ 40° C.
  • the fluid 70 does not vaporize during the exchange 109 .
  • This cycle 200 produces cold at between about ⁇ 100 and ⁇ 120° C. for the cryo-condensation 111 and between about 5° C. and ⁇ 100° C. in order to offset the deficit of cold during the exchange 109 .
  • Another part of the cold needed for the first cooling 109 is provided by an additional refrigerating cycle 181 , 183 , for example of the reverse Rankine type.
  • Another part of the cold needed for the second cooling 111 is provided by an additional refrigerating cycle 191 , 193 , for example of the reverse Rankine type.
  • the CO2-rich primary fluids 66 , 68 , 70 are compressed in stages 141 , 142 , 143 .
  • the first stages compress gaseous streams.
  • the compressed CO2 75 is cooled by an indirect-contact exchanger to convert it to liquid form. It is then mixed with the stream 73 .
  • This liquid mixture is pumped to the transport pressure (fluid 5 ).
  • the transport pressure is generally supercritical, the supercritical fluids will, by extension, be considered to be liquid at a temperature below that of the critical point for CO2.
  • FIGS. 2 to 7 which depict examples according to particular embodiments of the invention, do not depict the steps which apply to the process fluid 40 prior to its first cooling 109 , nor do they depict the compression of the CO2-rich primary fluids after the exchange of heat 109 . They depict only changes by comparison with FIG. 1 relating essentially to the refrigerating cycles that provide the cold for the exchanges 109 and 111 .
  • FIG. 2 illustrates an alternative form of the near-isentropic expansion with production of work, in which the working fluid is the CO2-lean gas 44 .
  • the cryo-condensation method is the same as in FIG. 1 . Only the changes are detailed below.
  • the CO2-lean gas 44 is compressed, for example by a multi-stage compressor 315 .
  • the fluid 303 is cooled if necessary to the inlet temperature for the exchanger 109 by the exchanger 316 .
  • This may be a direct-contact or an indirect-contact exchanger.
  • the compressed CO2-lean gas 304 is cooled in the exchanger 109 so that it can be expanded in the turbine 312 (near-isentropic expansion) so as to provide some of the cold needed for the exchange 111 .
  • the fluid 307 leaving the exchanger 111 is once again expanded (near-isentropic expansion) to provide work and cold for the exchanger 111 via the fluid 308 .
  • This loop in which the CO2-lean gas is expanded can be repeated as many times as necessary.
  • the CO2-lean gas 46 is heated up in the exchanger 109 .
  • the outgoing fluid 48 is processed like the fluid 48 in FIG. 1 .
  • Some of the cold needed for the exchanger 111 may be supplied by a refrigerating cycle 191 , 193 of the Rankine type.
  • FIG. 3 illustrates another alternative form of the near-isentropic expansion with the production of work.
  • the CO2-lean gas 44 gives up cold energy in the exchangers 111 and 109 . It is then compressed by the multi-stage compressor 415 . Next, it is cooled if necessary to the inlet temperature of the exchanger 109 in the exchanger 416 . This may be a direct-contact or an indirect-contact exchanger.
  • the CO2-lean gas 404 is once again cooled in the exchanger 109 before it is being expanded by the turbine 412 .
  • This near-isentropic turbine produces the cold required to compensate for part of the deficit of cold energy in the exchanger 111 .
  • the fluid 407 is expanded again by the near-isentropic turbine 414 .
  • the fluid 408 gives up its cold energy to compensate for part of the deficit of cold energy in the exchanger 111 .
  • This loop in which the CO2-lean gas is expanded can be repeated as many times as necessary.
  • the CO2-lean gas 46 is heated up in the exchanger 109 .
  • the outgoing fluid 48 is processed as the fluid 48 in FIG. 1 .
  • FIG. 4 illustrates another alternative form of the near-isentropic expansion with production of work.
  • the process fluid 40 is compressed by the compressor 512 which may be a multi-stage compressor.
  • the CO2-lean gas is expanded in a near-isentropic turbine 514 .
  • the temperature of the fluid 503 must remain above the cryo-condensation temperature for CO2.
  • FIG. 5 illustrates another alternative form of the near-isentropic expansion with the production of work, in which the working fluid is the process fluid.
  • This expansion turbine 612 needs to be designed with a great deal of care. It has to be suited to the high flow rates such as those of the flue gases 40 of an industrial plant, have very good isentropic efficiency, and be resistant to potential additional erosion due to the presence of solid CO2. To achieve this, carbon dioxide snow is allowed to be present in the rotor part of the turbine (the region contained between the leading edge 951 and the trailing edge 954 in FIGS. 14 and 15 ) and is forbidden or minimized in the stator part 960 upstream of the rotor part (the region contained upstream of the trailing edge of the stator vanes 950 ) in order notably not to cause erosion of the leading edge of the vanes 952 of the rotor part.
  • the CO2 it is preferable for the CO2 to be in the vapor or supersaturated vapor state in the stator part or for it to have carbon dioxide snow nucleii that are small enough (less than 10 ⁇ m, preferably 1 ⁇ m hydraulic diameter) to avoid eroding the rotor part.
  • This carbon dioxide snow is then separated from the CO2-lean gas in a separator 612 to obtain a solid comprising predominantly CO2 62 and a CO2-lean gas 44 .
  • This separation may be performed downstream of the rotor part by causing the fluid in the rotor part to rotate and by using the centrifugal effect to separate a CO2-rich fraction at the periphery from a CO2-lean fraction at the center. It may also be advantageous to increase the speed and therefore achieve an additional expansion of the fluid in a convergent nozzle 956 (a turbine known as a Laval turbine). By reducing the pressure before decelerating the gas the amount of solidified CO2 can be increased. Most of the CO2-lean gas is recovered at the center of the flow 959 and most of the solid CO2 is recovered at the periphery 958 , mixed in with a fraction of the gas.
  • an additional refrigerating cycle 191 , 193 of the Rankine type or which includes a near-isentropic expansion of a working fluid with or without the production of work provides the separator 612 with cold energy.
  • the solid 62 comprising predominantly CO2 is tipped into the liquid bath 121 and the next steps are the same as those depicted in FIG. 1 .
  • the CO2-lean gas 44 is heated up by exchange of heat with the process fluid in the exchanger 109 .
  • the fluid 605 is then compressed to a pressure higher than or equal to atmospheric pressure.
  • the outgoing fluid 48 is processed as in FIG. 1 .
  • FIG. 6 illustrates one embodiment with near-isentropic expansion without the production of work.
  • the process fluid 42 is still cooled to below the cryo-condensation temperature for CO2 in the vessel 111 to produce a cooled CO2-lean gas 701 . It is also possible for this vessel to be situated after the “expansion/Venturi” part 702 of the method, and will now be described.
  • Some of the CO2 to be captured solidifies in the form of a solid containing predominantly CO2 62 and is extracted from the vessel 111 .
  • the fluid 701 is made to rotate about an axis that is substantially parallel to the direction in which it flows using a system of fixed vanes 717 .
  • the stream 705 is made up predominantly of solid, although it may be necessary to separate the residual gas from the solid in a separator 731 .
  • the non-condensable part then gives up its cold energy in the exchangers 111 and 109 .
  • the solid comprising predominantly CO2 62 is tipped into the liquid bath 121 and undergoes the same steps as those described in FIG. 1 .
  • the streams 48 are used to cool the water, in the same way as the stream 50 in FIG. 1 .
  • FIG. 7 illustrates another embodiment with near-isentropic expansion without the production of work.
  • the exchange 809 comprises the same features as the exchange 109 in FIG. 1 .
  • the exchanger 811 cools the process fluid 42 to a temperature below the liquefaction temperature of CO2. From this there emerges a cooled process fluid 801 which is sent to a separator 812 .
  • a CO2-rich liquid 816 is extracted by the separator 812 .
  • the residual fluid 802 is made to rotate about an axis substantially parallel to the direction in which it flows by a system of fixed vanes 817 . It is expanded as it leaves 803 the vanes having been rotated and cooled to below the cryo-condensation temperature for CO2 without producing work. The expansion may take place through a Venturi effect by passing the fluid through a restriction 818 .
  • the stream 805 is made up predominantly of solid, although it may be necessary to separate the residual gas from the solid in a separator 841 .
  • the non-condensables 44 give up their cold energy in the exchangers 811 and 809 .
  • a second (or even a third or more) step in which the fluid 806 undergoes a near-isentropic expansion with Venturi effect may be added. This step is identical to the previous one:
  • the solid 62 comprising predominantly CO2 recovered at the outlet from the separators 841 and possibly 851 is tipped into the liquid bath 121 and processed as in FIG. 1 .
  • Streams 48 are used to cool the water, in the same way as the stream 50 in FIG. 1 .
  • FIG. 8 depicts a plant for producing the electricity from coal, employing various units 4 , 5 , 6 and 7 for purifying the flue gases 19 .
  • a primary airflow 15 passes through the unit 3 in which the coal 15 is pulverized and carried along toward the burners of the boiler 1 .
  • a secondary airflow 16 is applied directly to the burners in order to provide additional oxygen needed for near-complete combustion of the coal.
  • Feed water 17 is sent to the boiler 1 to produce steam 18 which is expanded in a turbine 8 .
  • FIG. 9 depicts a plant for producing electricity from coal, implementing various units 5 and 7 for purifying the flue gases 19 .
  • a primary airflow 15 passes through the unit 3 where the coal 15 is pulverized and carried along toward the burners of the boiler 1 .
  • a secondary flow of oxidant 16 is supplied directly to the burners in order to provide the additional oxygen needed for near-complete combustion of the coal. This secondary oxidant is the result of the mixing of flue gases 94 recirculated using a blower 91 with oxygen 90 produced by a unit 10 for separating air gases.
  • Feed water 17 is sent to the boiler 1 to produce steam 18 which is expanded in a turbine 8 .
  • the fluid 93 may be in liquid, gaseous or diphasic form and consists of a mixture of cooled air gases.
  • this may be cold gaseous nitrogen or air (at between ⁇ 56° C. and ⁇ 196° C.), or alternatively liquid nitrogen or air. It is intended to be introduced into the vessel referenced 111 in FIGS. 1 to 4 and in FIG. 6 , referenced 612 in FIG. 5 , 731 in FIGS. 6 , and 841 , 851 in FIG. 7 .
  • the unit 7 may also produce a fluid 92 which will be used in the unit for separating air gases.
  • This may, for example, be a fraction of the lean gas leaving the vessel 111 in FIGS. 1 to 4 and 6 , 612 in FIG. 5 , 731 in FIGS. 7 and 841 , 851 in FIG. 8 .
  • This lean gas in some way restores cold to the unit 10 at a temperature level higher than that afforded from the unit 10 by the fluid 93 .
  • the time at which the cold is produced by the unit 10 (for example liquid nitrogen) is separated from the time at which it is used in the unit 7 .
  • the near-isentropic expansion of a gas can be carried out in the unit 10 rather than in the unit 7 .
  • This scheme may prove well suited to instances where existing plants are being modified, where replacing the primary air sent to the coal pulverizers with a mixture of recirculated flue gases plus oxygen could prove complicated, partly because of the increase in water content, the flue gases containing far more water than damp air, and partly for safety reasons, although that should not be overestimated.
  • FIG. 10 schematically depicts the use of a method according to the invention in a steel-making plant.
  • a unit 10 for separating the air gases supplies oxygen 90 to a blast furnace 900 into which iron ore 901 and carbon products 902 (coal and coke) are also introduced.
  • the blast furnace in that instance operates in the presence of little nitrogen.
  • the blast furnace gases 903 made up for example of 47% CO, 36% CO2, 8% N2 and 9% other compounds such as H2 and H2O can be split into two.
  • Most 905 goes to the CO2 capture unit with another proportion 904 used to reduce the nitrogen concentration in the loop.
  • the fluid 905 is cooled beforehand in a direct-contact exchanger 906 , has its dust removed in the filter 103 , and is then compressed by a compressor 901 , is cooled in an exchanger 105 and dried in a drier 107 before entering the low-temperature exchanger 109 where it will be cooled and then partially liquefied to a temperature close to the triple point for CO2 without the formation of solid.
  • the diphasic gas-liquid fluid 912 obtained is separated into a gaseous fraction 502 and a liquid fraction 920 in the separator 928 .
  • the gaseous fraction 502 is then cooled by near-isentropic expansion, for example in a turbine 514 , so as to obtain a diphasic gas-solid fluid 503 .
  • This is separated in the vessel 111 into a gaseous fraction 44 and a CO2-rich solid fraction 62 .
  • the solid fraction 62 is compressed, for example by an endless screw and mixed with the liquid 920 in the bath 121 , which is heated by gas 72 produced by vaporizing liquid 74 in the exchanger 109 .
  • the liquid CO2 64 is compressed by a pump 69 to obtain a pressurized liquid 70 and is heated up in the exchanger 109 without undergoing vaporization or pseudo-vaporization if the pressure is above the supercritical pressure.
  • the lean gas is successively heated up by a compressor 315 and by the exchanger 109 .
  • the invention may also be adapted to types of blast furnace operating on enriched air, for example by adding a CO/N2 separation using cryogenic distillation, cooling the gas 44 to the required temperature.
  • FIG. 11 schematically depicts the use of a method according to the invention in a plant for producing synthesis gas from an oxygen process (partial oxidation, gasification, auto-thermal reformer, etc.).
  • a unit 10 for separating air gases supplies oxygen 90 to a reactor 900 into which a carbon product 902 (coal, natural gas, biomass, household waste, etc.) is introduced.
  • the synthesis gases 903 chiefly comprise the compounds CO, CO2, H2 and H2O.
  • the CO can be converted (in a so-called shift reaction) into CO2 and H2 in the presence of water vapor: CO+H2O ⁇ >CO2+H2 in the unit 907 .
  • This unit may also include one or more exchangers for cooling the gas prior to compression.
  • the fluid 905 may possibly have its dust removed in a filter 103 , then be compressed by a compressor 101 , cooled in an exchanger 105 and dried in a dryer 107 before entering the low-temperature exchanger 109 where it may be partially liquefied at a temperature close to that of the triple point for CO2.
  • This diphasic gas-liquid fluid 912 is separated into a gaseous fraction 502 and a liquid fraction 920 in the separator 928 .
  • the gaseous fraction 502 is then cooled by near-isentropic expansion, for example in a turbine 514 , to obtain a diphasic gas-solid stream 503 .
  • This is separated into a gaseous fraction 44 and a CO2-rich solid fraction 62 in the vessel 111 .
  • the solid fraction 62 is mixed with the liquid 920 in the bath 121 , which is heated with gas 74 produced by the vaporizing of the liquid 72 in the exchanger 109 .
  • the liquid CO2 64 is compressed by a pump and heated up in the exchanger 109 without vaporizing, or pseudo-vaporizing if the pressure is above the supercritical pressure.
  • the lean gas 44 is successively heated up via a compressor 924 and the exchanger 109 .
  • This lean gas essentially consisting of hydrogen may be sent to a gas turbine to be combusted without the emission of CO2.
  • the unit 10 may supply hot nitrogen 90 a which is introduced downstream of the dryers 910 , and/or cold nitrogen 90 b, introduced directly into the vessel 111 to increase the amount of CO2 captured.
  • the expansion in the turbine 514 of the hot nitrogen present in the stream 502 provides additional cold energy for solid cryo-condensation of CO2 in the turbine 514 ; in the second instance, the cold nitrogen 90 b, by heating up upon contact with the fluid 503 , leads to solid cryo-condensation of the CO2.
  • the other benefit of hot nitrogen 90 a is that it increases the molecular weight of the gas 502 , something that may prove advantageous in reducing the cost of the expansion 514 and/or of the compression 924 . What actually happens is that when these gases are very rich in hydrogen, it is not easy for these gases to be compressed/expanded using the technologies best suited to high flow rates, namely technologies of the axial, radial or supersonic shockwave type. It then becomes necessary to use technologies of the positive-displacement type, for example using pistons or screws, which are very expensive to implement.
  • FIG. 12 schematically depicts the use of a method according to the invention in a plant producing synthesis gas from steam reforming.
  • a carbon product 902 (natural gas, methanol, naphtha, etc.) is introduced into a reactor 900 .
  • the synthesis gases 903 produced in the reactor 900 chiefly comprise the compounds CO, CO2, H2 and H2O.
  • the fluid 905 may potentially be compressed by a compressor 101 , cooled in an exchanger 105 and dried in a dryer 107 before entering a low-temperature exchanger 109 where it may be partially liquefied at a temperature close to that of the triple point for CO2.
  • the diphasic gas-liquid fluid 912 obtained is separated into a gaseous fraction 502 and a liquid fraction 920 in the separator 928 .
  • the gaseous fraction 502 is then cooled by a near-isentropic expansion, for example in a turbine 514 , so as to obtain a gas-solid diphasic mixture 503 .
  • the solid fraction 62 is mixed with the liquid 920 in the bath 121 , which is heated with gas 74 produced by the vaporizing of the liquid 72 in the exchanger 109 .
  • the liquid CO2 64 is compressed by a pump and heated up in the exchanger 109 without vaporizing or pseudo-vaporizing if the pressure is above the supercritical pressure.
  • the lean gas 44 can then be purified in terms of CO2 at a low temperature, for example by adsorption using a molecular sieve 13 X before being introduced into a cryogenic unit 924 for the production of CO.
  • This unit operates, for example, by methane scrubbing or partial condensation of the CO.
  • This unit 924 produces a hydrogen-enriched gas 929 and a CO-enriched gas 925 .
  • One or more fluids of this unit may be compressed at low temperature, then reintroduced into the heat exchanger 926
  • solid cryo-condensation replaces elimination of CO2 by absorption with amines (MDEA or MEA). If there is a desire to produce pure hydrogen, then it is possible to add an H2 PSA into this scheme either upstream of this solid cryo-condensation purification, that is to say on the outlet side of the reformer 900 after the cooling of the synthesis gas, or on the H2-rich gas 929 .
  • FIG. 13 schematically depicts an alternative form of the invention combined with a method implementing a transcritical Rankine cycle on the CO2. It also includes the features of a method in which a liquid cryo-condensation and then a solid cryo-condensation are performed in succession and in which the purity of the CO2 produced is improved using two distillation columns, one of them to eliminate the compounds less volatile than CO2 (NO2 or N204, SO2, etc.) and another to eliminate the compounds that are more volatile.
  • the fluid 24 consists of flue gases and may be at a temperature of the order of 150° C. and is injected into a filter 103 to remove the particles down to a concentration level of below 1 mg/m 3 , preferably below 100 ⁇ g/m 3 .
  • the dust-free fluid 30 is cooled to a temperature of close to 0° C., generally of between 0° C. and 10° C., so as to condense the water vapor it contains.
  • This cooling is carried out in a tower 105 b, with water injected at two levels, cold water 36 b and water 34 b at a temperature close to the wet bulb temperature of the ambient air. It is also possible to conceive of indirect contact.
  • the tower 105 may or may not have packings. This tower may also serve as a scrubbing tower for the SO2.
  • the fluid that may have been desaturated is compressed to a pressure of between 5 and 50 bar abs in the compressor 101 .
  • the fluid 32 is cooled to a temperature close to 0° C. and generally of between 0° C. and 10° C. so as to condense the water vapor it contains.
  • This cooling is carried out in a tower 105 with water injected at two levels, cold water 36 and water 34 at a temperature close to the wet bulb temperature of the ambient air. It is also possible to conceive of indirect contact.
  • the tower 105 may or may not have packings.
  • the fluid 38 is sent to a unit 107 that eliminates the residual water vapor, for example using one and/or another of the following methods:
  • the process fluid 40 is cooled then brought into contact in a distillation column 79 with pure CO2, so as to recover the compounds less volatile than CO2 in the form of a liquid containing CO2 and, for example, NO2 (or its dimer N2O4).
  • This liquid can be pumped and vaporized in the unit 78 , then sent either to a combustion chamber to reduce the NO2 or to the unit for purifying the stream 30 by low-pressure scrubbing of the SO2, where it acts as a reagent, either directly in the form of NO2 or in the form of nitric acid having been reacted with water.
  • the process fluid 74 a is then cooled and partially condensed into liquid form and sent to the separator 76 .
  • the liquid fraction 76 a is sent to the bath 121 .
  • the gaseous fraction 76 b is sent to an expansion turbine so as there to produce a gas-solid diphasic stream 42 which is then sent to the vessel 111 where it is separated into a CO2-lean gas 44 and solid CO2 62 .
  • An auxiliary fluid 93 for example from an air gas separation unit, may potentially supply additional cold for solid cryo-condensation. When it does, it may be advantageous to tap from the CO2-lean gas 44 a fluid 92 which returns to the unit that supplied the fluid 93 .
  • the solid 62 is compressed for example by an endless screw and injected into the bath 121 of liquid CO2, from which a liquid 64 is tapped.
  • This liquid may potentially be pumped and introduced into a distillation column 75 where its compounds more volatile than CO2 are eliminated.
  • the pure liquid 68 is heated up without vaporizing or pseudo-vaporizing if it is supercritical. It may once again be pumped to obtain the fluid 5 ready for transport.
  • a part of the fluid 5 may be tapped off to be vaporized or pseudo-vaporized in a unit 72 .
  • This unit 72 is, for example, any arbitrary source of heat of the plant that produces the process fluid.
  • This part of the fluid 80 is then expanded in a turbine 73 used to produce electricity or mechanical power and is then cooled in the exchanger 109 and condensed by direct exchange in the bath 121 , at the same time melting the solid CO2.
  • the fluid 48 can still notably be used to regenerate the unit that eliminates residual vapor 107 and/or for producing cold water 36 a by evaporation in a direct-contact tower 115 into which a dry fluid 50 is introduced and becomes saturated with water, vaporizing part of it.
  • the cold water may undergo additional cooling in a refrigerating unit 119 . Thereafter, this cold water can be used in one and/or other of the towers 105 and 105 b to cool the process gas before and/or after compression.
  • FIGS. 14 and 15 depict a turbine for carrying out near-isentropic expansion of the process fluid with the production of external work in accordance with the invention.
  • the upstream stator part 960 begins with the volute (not depicted) followed by vanes 950 which may be fixed or variable.
  • the rotor part 960 which, for example, comprises blades 952 with a leading edge 951 where the rotor part 960 begins and a trailing edge 954 where it ends.
  • the rotor part Downstream of the rotor part, if centrifugal force is not to be used on the solid parts, the rotor part may consist of a simple deceleration cone.
  • downstream stator part 961 is to be used to achieve a first separation, then the fact that the fluid has been made to rotate in the rotor part and the centrifugal effect can be used to separate a CO2-rich fraction at the periphery from a CO2-lean fraction at the center. It may also be advantageous to increase the speed and therefore perform an additional expansion of the fluid in a convergent nozzle 956 (a so-called “Laval” turbine). By reducing the pressure before decelerating the gas, the amount of solidified CO2 can be increased. Most of the CO2-lean gas is recovered at the center of the flow 959 and most of the solid CO2 is recovered at the periphery 958 , mixed in with a fraction of gas.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Treating Waste Gases (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US13/133,448 2008-12-19 2009-12-14 CO2 Recovery And Cold Water Production Method Abandoned US20110252827A1 (en)

Applications Claiming Priority (3)

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FR0858866A FR2940413B1 (fr) 2008-12-19 2008-12-19 Procede de capture du co2 par cryo-condensation
FR0858866 2008-12-19
PCT/FR2009/052509 WO2010076467A1 (fr) 2008-12-19 2009-12-14 Procédé de capture du co2 et de production d'eau froide

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US13/133,543 Abandoned US20110302955A1 (en) 2008-12-19 2009-12-14 Method For Trapping CO2 By Solid Cryocondensation In A Turbine
US13/133,448 Abandoned US20110252827A1 (en) 2008-12-19 2009-12-14 CO2 Recovery And Cold Water Production Method

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US13/133,543 Abandoned US20110302955A1 (en) 2008-12-19 2009-12-14 Method For Trapping CO2 By Solid Cryocondensation In A Turbine

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Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120023947A1 (en) * 2010-07-30 2012-02-02 General Electric Company Systems and methods for co2 capture
US20120137698A1 (en) * 2009-07-13 2012-06-07 Sjoedin Mats Cogeneration plant and cogeneration method
US20120297821A1 (en) * 2011-05-26 2012-11-29 Brigham Young University Systems and methods for separating condensable vapors from light gases or liquids by recruperative cryogenic processes
US20130025294A1 (en) * 2011-07-28 2013-01-31 Christian Vogel System and method for carbon dioxide removal
US20130074541A1 (en) * 2010-02-03 2013-03-28 Robert D. Kaminsky Systems and Methods For Using Cold Liquid To Remove Solidifiable Gas Components From Process Gas Streams
US20130084794A1 (en) * 2011-09-29 2013-04-04 Vitali Victor Lissianski Systems and methods for providing utilities and carbon dioxide
CN103086375A (zh) * 2011-11-04 2013-05-08 气体产品与化学公司 二氧化碳的纯化
EP2596846A1 (fr) * 2011-11-22 2013-05-29 General Electric Company Expanseur et procédé pour la séparation du CO2
US20130239608A1 (en) * 2011-11-22 2013-09-19 General Electric Company System and method for separating components in a gas stream
US20130283852A1 (en) * 2012-04-26 2013-10-31 General Electric Company Method and systems for co2 separation
US20140144178A1 (en) * 2012-11-28 2014-05-29 L'Air Liquide Societe Anonyme Pour L'Etude Et L'Expoitation Des Procedes Georges Claude Optimized heat exchange in a co2 de-sublimation process
US20140208798A1 (en) * 2011-05-31 2014-07-31 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Apparatus and Integrated Process for Separating a Mixture of Carbon Dioxide and at Least One Other Gas and for Separating Air by Cryogenic Distillation
US20150033792A1 (en) * 2013-07-31 2015-02-05 General Electric Company System and integrated process for liquid natural gas production
WO2018129038A1 (fr) * 2017-01-05 2018-07-12 Larry Baxter Dispositif de séparation de dioxyde de carbone solide à partir d'une suspension
US20190063825A1 (en) * 2017-08-24 2019-02-28 Donald J. Victory Method and System for LNG Production using Standardized Multi-Shaft Gas Turbines, Compressors and Refrigerant Systems
US10473029B2 (en) * 2013-12-30 2019-11-12 William M. Conlon Liquid air power and storage
US10738696B2 (en) * 2015-06-03 2020-08-11 William M. Conlon Liquid air power and storage with carbon capture
US11486638B2 (en) 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method
CN115382339A (zh) * 2022-07-26 2022-11-25 中国石油大学(华东) 用于工业制氢的超音速碳捕集能量回收装置及系统
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Publication number Priority date Publication date Assignee Title
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EP2505948B1 (fr) * 2011-03-30 2018-10-10 General Electric Technology GmbH Séparation cryogénique de CO2 au moyen d'un système de réfrigération
US20130025317A1 (en) * 2011-06-15 2013-01-31 L'Air Liguide Societe Anonyme Pour L' Etude Et L' Exploitation Des Procedes Georges Claude Process for Removing Carbon Dioxide From a Gas Stream using Desublimation
FR2988166B1 (fr) * 2012-03-13 2014-04-11 Air Liquide Procede et appareil de condensation d'un debit gazeux riche en dioxyde de carbone
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CN102606240A (zh) * 2012-03-27 2012-07-25 中国科学院微电子研究所 一种利用co2发电的系统及方法
FR2992056B1 (fr) * 2012-06-15 2018-11-09 L'air Liquide,Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de refroidissement ou de rechauffage d'un melange gazeux
FR2993353B1 (fr) * 2012-07-13 2018-06-15 Air Liquide Procede et appareil de purification d'un melange riche en dioxyde de carbone a basse temperature
CN103344090B (zh) * 2013-06-19 2016-06-22 曲昭波 液化空气制冷和灭火系统
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NL2013653B1 (en) * 2014-10-20 2016-10-04 Haffmans Bv A process installation for preparing a carbon dioxide (CO2) end product from a gaseous carbon dioxide containing starting product.
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JP6776154B2 (ja) * 2017-02-27 2020-10-28 三菱重工マリンマシナリ株式会社 ラジアルタービン、ラジアルタービンの排気部材
JP7434334B2 (ja) * 2019-01-25 2024-02-20 サウジ アラビアン オイル カンパニー Ｃｏ２回収を伴って水素を生成するための液体炭化水素およびｃｏ２輸送のためのプロセスおよび方法
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EP4491258A1 (fr) * 2023-07-14 2025-01-15 Linde GmbH Procédé et installation de refroidissement d'un gaz de processus
US20250198698A1 (en) * 2023-12-19 2025-06-19 Southwest Research Institute Cryogenic-Based Carbon Dioxide Capture System

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6053007A (en) * 1997-07-01 2000-04-25 Exxonmobil Upstream Research Company Process for separating a multi-component gas stream containing at least one freezable component
US6321566B1 (en) * 1999-05-21 2001-11-27 Kabushiki Kaisha Kobe Seiko Sho. Method for producing oxygen gas
US20070292306A1 (en) * 2004-03-02 2007-12-20 Yoshio Hirano Method and System of Removing Moisture and Toxic Gas Components from Exhaust Gas
US20080072762A1 (en) * 2004-08-06 2008-03-27 Eli Gal Ultra Cleaning of Combustion Gas Including the Removal of Co2
US20080178733A1 (en) * 2007-01-31 2008-07-31 Eli Gal Use of so2 from flue gas for acid wash of ammonia

Family Cites Families (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB771405A (en) * 1954-06-01 1957-04-03 Union Carbide & Carbon Corp Improvements in the cold separation of air
US3614872A (en) * 1967-12-22 1971-10-26 Texaco Inc Synthesis gas separation process
US4791784A (en) * 1985-06-17 1988-12-20 University Of Dayton Internal bypass gas turbine engines with blade cooling
JPH0914831A (ja) * 1995-06-27 1997-01-17 Mitsubishi Heavy Ind Ltd Ｃｏ２ 回収装置及び回収方法
TW366409B (en) * 1997-07-01 1999-08-11 Exxon Production Research Co Process for liquefying a natural gas stream containing at least one freezable component
WO2000023757A1 (fr) * 1998-10-16 2000-04-27 Translang Technologies Ltd. Tube tourbillon destine a la liquefaction et a la separation de constituants dans un melange gazeux
US6082133A (en) * 1999-02-05 2000-07-04 Cryo Fuel Systems, Inc Apparatus and method for purifying natural gas via cryogenic separation
DE19940371A1 (de) * 1999-08-25 2001-03-01 Messer Griesheim Gmbh Verfahren und Vorrichtung zur Gewinnung von Kohlendioxid aus Abgasen
FR2820052B1 (fr) 2001-01-30 2003-11-28 Armines Ass Pour La Rech Et Le Procede d'extraction du dioxyde de carbone par anti-sublimation en vue de son stockage
JP4979138B2 (ja) * 2001-01-31 2012-07-18 株式会社前川製作所 ドライアイス製造方法とその装置
US20020189443A1 (en) * 2001-06-19 2002-12-19 Mcguire Patrick L. Method of removing carbon dioxide or hydrogen sulfide from a gas
US6884507B2 (en) * 2001-10-05 2005-04-26 General Electric Company Use of high modulus, impact resistant foams for structural components
FR2851936B1 (fr) * 2003-03-04 2006-12-08 Procede d'extraction du dioxyde de carbone et du dioxyde de soufre par anti-sublimation en vue de leur stockage
CN1956768A (zh) * 2004-03-02 2007-05-02 中国电力株式会社 处理废气的方法和系统，和分离二氧化碳的方法和装置
RU2272973C1 (ru) * 2004-09-24 2006-03-27 Салават Зайнетдинович Имаев Способ низкотемпературной сепарации газа (варианты)
JP2006117458A (ja) * 2004-10-20 2006-05-11 Mitsubishi Heavy Ind Ltd ドライアイス製造システム
FR2880677B1 (fr) 2005-01-07 2012-10-12 Air Liquide Procede de pretraitement de l'air avant introduction dans une unite de separation d'air par voie cryogenique et appareil correspondant
FR2894838B1 (fr) * 2005-12-21 2008-03-14 Gaz De France Sa Procede et systeme de capture du dioxyde de carbone present dans des fumees
US8038388B2 (en) * 2007-03-05 2011-10-18 United Technologies Corporation Abradable component for a gas turbine engine

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6053007A (en) * 1997-07-01 2000-04-25 Exxonmobil Upstream Research Company Process for separating a multi-component gas stream containing at least one freezable component
US6321566B1 (en) * 1999-05-21 2001-11-27 Kabushiki Kaisha Kobe Seiko Sho. Method for producing oxygen gas
US20070292306A1 (en) * 2004-03-02 2007-12-20 Yoshio Hirano Method and System of Removing Moisture and Toxic Gas Components from Exhaust Gas
US20080072762A1 (en) * 2004-08-06 2008-03-27 Eli Gal Ultra Cleaning of Combustion Gas Including the Removal of Co2
US20080178733A1 (en) * 2007-01-31 2008-07-31 Eli Gal Use of so2 from flue gas for acid wash of ammonia

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Duncan Barker et al., CO2 Capture in Cement Industry, July 2008, Mott MacDonald Ltd, page "4-30" and page "4-31" *

Cited By (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120137698A1 (en) * 2009-07-13 2012-06-07 Sjoedin Mats Cogeneration plant and cogeneration method
US9657604B2 (en) * 2009-07-13 2017-05-23 Siemens Aktiengesellschaft Cogeneration plant with a division module recirculating with a first combustion gas flow and separating carbon dioxide with a second combustion gas flow
US20130074541A1 (en) * 2010-02-03 2013-03-28 Robert D. Kaminsky Systems and Methods For Using Cold Liquid To Remove Solidifiable Gas Components From Process Gas Streams
US11112172B2 (en) 2010-02-03 2021-09-07 Exxonmobil Upstream Research Company Systems and methods for using cold liquid to remove solidifiable gas components from process gas streams
US10408534B2 (en) * 2010-02-03 2019-09-10 Exxonmobil Upstream Research Company Systems and methods for using cold liquid to remove solidifiable gas components from process gas streams
US20120023947A1 (en) * 2010-07-30 2012-02-02 General Electric Company Systems and methods for co2 capture
US20120297821A1 (en) * 2011-05-26 2012-11-29 Brigham Young University Systems and methods for separating condensable vapors from light gases or liquids by recruperative cryogenic processes
US10724793B2 (en) * 2011-05-26 2020-07-28 Hall Labs Llc Systems and methods for separating condensable vapors from light gases or liquids by recuperative cryogenic processes
US20140208798A1 (en) * 2011-05-31 2014-07-31 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Apparatus and Integrated Process for Separating a Mixture of Carbon Dioxide and at Least One Other Gas and for Separating Air by Cryogenic Distillation
US20130025294A1 (en) * 2011-07-28 2013-01-31 Christian Vogel System and method for carbon dioxide removal
US20130084794A1 (en) * 2011-09-29 2013-04-04 Vitali Victor Lissianski Systems and methods for providing utilities and carbon dioxide
CN103086375A (zh) * 2011-11-04 2013-05-08 气体产品与化学公司 二氧化碳的纯化
EP2596846A1 (fr) * 2011-11-22 2013-05-29 General Electric Company Expanseur et procédé pour la séparation du CO2
CN103134268A (zh) * 2011-11-22 2013-06-05 通用电气公司 用于二氧化碳分离的膨胀机和方法
US20130239608A1 (en) * 2011-11-22 2013-09-19 General Electric Company System and method for separating components in a gas stream
US20130283852A1 (en) * 2012-04-26 2013-10-31 General Electric Company Method and systems for co2 separation
US20140144178A1 (en) * 2012-11-28 2014-05-29 L'Air Liquide Societe Anonyme Pour L'Etude Et L'Expoitation Des Procedes Georges Claude Optimized heat exchange in a co2 de-sublimation process
US20150033792A1 (en) * 2013-07-31 2015-02-05 General Electric Company System and integrated process for liquid natural gas production
US12385432B2 (en) * 2013-12-30 2025-08-12 Pintail Power Llc Liquid air power and storage
US20240328350A1 (en) * 2013-12-30 2024-10-03 Pintail Power Llc Liquid air power and storage
US10473029B2 (en) * 2013-12-30 2019-11-12 William M. Conlon Liquid air power and storage
US20200095932A1 (en) * 2013-12-30 2020-03-26 William M. Conlon Liquid air power and storage
US10738696B2 (en) * 2015-06-03 2020-08-11 William M. Conlon Liquid air power and storage with carbon capture
WO2018129038A1 (fr) * 2017-01-05 2018-07-12 Larry Baxter Dispositif de séparation de dioxyde de carbone solide à partir d'une suspension
US11105553B2 (en) * 2017-08-24 2021-08-31 Exxonmobil Upstream Research Company Method and system for LNG production using standardized multi-shaft gas turbines, compressors and refrigerant systems
US20190063825A1 (en) * 2017-08-24 2019-02-28 Donald J. Victory Method and System for LNG Production using Standardized Multi-Shaft Gas Turbines, Compressors and Refrigerant Systems
US11486638B2 (en) 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method
CN115382339A (zh) * 2022-07-26 2022-11-25 中国石油大学(华东) 用于工业制氢的超音速碳捕集能量回收装置及系统
WO2025212518A1 (fr) * 2024-04-01 2025-10-09 Carbon Capture America, Inc Procédés, systèmes et appareil de traitement de flux gazeux comprenant du dioxyde de carbone

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CN102317726A (zh) 2012-01-11
EP2379971B1 (fr) 2014-02-12
FR2940413B1 (fr) 2013-01-11
WO2010070226A1 (fr) 2010-06-24
EP2379970A1 (fr) 2011-10-26
CN102317207A (zh) 2012-01-11
US20110296868A1 (en) 2011-12-08
CN102326044A (zh) 2012-01-18
WO2010076467A1 (fr) 2010-07-08
FR2940413A1 (fr) 2010-06-25
EP2379971A1 (fr) 2011-10-26
EP2379199A1 (fr) 2011-10-26
CN102326044B (zh) 2015-08-19
US20110302955A1 (en) 2011-12-15
WO2010076466A1 (fr) 2010-07-08

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