EP2641043A2 - Method and appliance for purifying a flow rich in carbon dioxide - Google Patents

Method and appliance for purifying a flow rich in carbon dioxide

Info

Publication number
EP2641043A2
EP2641043A2 EP11794550.1A EP11794550A EP2641043A2 EP 2641043 A2 EP2641043 A2 EP 2641043A2 EP 11794550 A EP11794550 A EP 11794550A EP 2641043 A2 EP2641043 A2 EP 2641043A2
Authority
EP
European Patent Office
Prior art keywords
liquid
phase separator
pressure
enclosure
carbon dioxide
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11794550.1A
Other languages
German (de)
French (fr)
Inventor
Alain Briglia
Philippe Court
Arthur Darde
Ludovic Granados
Jean-Pierre Tranier
Xavier Traversac
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from FR1059389A external-priority patent/FR2967485B1/en
Priority claimed from FR1156755A external-priority patent/FR2974361A1/en
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP2641043A2 publication Critical patent/EP2641043A2/en
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • F25J3/0266—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
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/0625—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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation 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
    • B01D2256/22—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
    • 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
    • F25J2200/70—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
    • 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
    • F25J2230/30—Compression of 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/80—Quasi-closed internal or closed external carbon dioxide refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
    • 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 and apparatus for purifying a flow rich in carbon dioxide.
  • a flow rich in carbon dioxide contains at least 20% vol. carbon dioxide, or at least 40% vol. of carbon dioxide, or at least 50% vol of carbon dioxide or even at least 60% vol. or at least 70% vol. of carbon dioxide.
  • the flow is cooled and partially condensed.
  • the liquid phase thus formed is enriched in carbon dioxide and the gaseous phase is enriched in at least one lighter component that can be oxygen, nitrogen, argon, carbon monoxide, hydrogen , methane etc. according to the composition of the flow to be purified.
  • a purification apparatus of a flow rich in carbon dioxide known from
  • WO-A-20090007937 comprises a plurality of phase separators, two of which are connected in series.
  • the apparatus may comprise at least two phase separators operating at different pressures to improve the efficiency of the separation.
  • the flow is cooled in a heat exchanger and partially condensed ii) the partially condensed flow is sent to a first phase separator operating at a first pressure
  • a gas of the first phase separator is heated, compressed, cooled and sent to a second phase separator operating at a second pressure greater than the first pressure
  • a first liquid is expanded and sent from the first phase separator to an enclosure operating at a pressure lower than the first pressure
  • a second liquid from the second phase separator or a third liquid derived from the second liquid is expanded and sent to the enclosure
  • the liquid sent from the first phase separator to the chamber may be composed of the first liquid and the third liquid mixed, as illustrated in FIG. 3.
  • the third liquid is derived from the second liquid by separation in the first phase separator.
  • the second liquid is heated, possibly in the heat exchanger, and then expanded in a valve to the pressure of the chamber and sent to the enclosure.
  • the second phase separator operates at a lower pressure than the inlet of the second liquid in the exchanger, because of a hydrostatic pressure due to the position of the second phase separator above the inlet of the second liquid in the exchanger.
  • the second liquid is first expanded to an intermediate pressure between the second pressure and the pressure of the chamber and then to the pressure of the chamber.
  • the second liquid is expanded to the first pressure, sent to the first phase separator and the third liquid derived from the second liquid is sent from the first phase separator to the enclosure
  • the enclosure is a phase separator.
  • the enclosure is a distillation or washing column.
  • the inlet temperature of the compressor is substantially equal to the temperature of the inlet of the flow rate to be cooled in the heat exchanger.
  • a device for purifying a flow rich in carbon dioxide and containing at least one lighter impurity than carbon dioxide comprising an enclosure, a compressor, a first phase separator a second phase separator, a heat exchanger, a pipe for sending the carbon dioxide-rich flow to be cooled in the heat exchanger, a pipe for bringing the cooled flow rate of the exchanger to the first phase separator, means for feeding a gas from the first phase separator to the heat exchanger for heating, means for supplying this gas from the heat exchanger to the compressor, a pipe for supplying the compressor gas to the heat exchanger, a pipe for bringing the compressed gas from the heat exchanger to the second phase separator , a pipe for bringing a first liquid of the first phase separator to the enclosure, a valve for expanding the first liquid upstream of the enclosure, a pipe for discharging a purified liquid rich in carbon dioxide from the enclosure and
  • the means for withdrawing the second liquid from the second phase separator and for bringing the second liquid to the chamber are constituted by a pipe connected to an inlet point of the exchanger and to the second phase separator and a pipe connected to an intermediate point of the exchanger and the enclosure.
  • the point of entry of the exchanger is below the point of withdrawal of the second liquid from the second phase separator.
  • the apparatus comprises means for expanding the second liquid at an intermediate pressure lower than the operating pressure of the second phase separator and means for expanding the second liquid or a third liquid derived from the second liquid at the pressure of the second pregnant.
  • the apparatus comprises means connecting the second phase separator to the first phase separator to allow the passage of liquid.
  • the enclosure is a distillation or washing column.
  • the enclosure is a third separator pot.
  • the gas of a first phase separator can be compressed to a higher pressure and recondensed, possibly at the same temperature.
  • a distillation column may be needed.
  • all liquid flows from the phase separators are expanded and fed to a phase separator or distillation column.
  • the liquid that cools during relaxation can then solidify.
  • the basic solution is to avoid overheating the flow at higher pressure so that the liquid phase can be relaxed without risk.
  • This approach reduces the carbon dioxide yield of the process as it reduces the pressure and temperature of a partial condensation.
  • phase separators and the heat exchanger it is envisaged to install the phase separators and the heat exchanger so that there is sufficient hydrostatic head to prevent the vaporization of the liquid. If the liquid of the separator is heated, even a little, at the same pressure, it will begin to vaporize immediately. Higher pressure is required for the liquid to remain liquid at the higher temperature.
  • Yet another solution is to relax at least one of the liquids at the highest pressure in stages.
  • One possibility is to relax the liquid at higher pressure in an intermediate phase separator whose liquid is sent to the column.
  • An advantage of this solution is that it reduces the number of pipes in the cold box and the number of connections to the column and the number of connections on the main exchanger and finally the arrangement constraints related to hydrostatic head requirements. .
  • Figures 1 to 4 show apparatus according to the invention.
  • a compressor 1 compresses a flow rich in carbon dioxide, containing at least 20% vol carbon dioxide, or even at least 40% vol carbon dioxide, possibly at least 60% vol carbon dioxide and at least one light impurity which may be oxygen, nitrogen, argon, carbon monoxide, hydrogen, methane or several of these impurities.
  • the flow can come for example from an oxycombustion, a steel plant, a cement plant, a SMR ...
  • the flow After compression at a pressure between 8 and 40 bar a, the flow is cooled in the cooler 4, purified with water in the adsorption unit 5 and then sent to cool in the exchange line 7 which can be constituted by a plate and fin heat exchanger aluminum arm é.
  • the cooled and partially condensed flow rate is sent to a first phase separator 9.
  • the first liquid 1 1 of the first phase separator 9 is expanded in a valve 13 and then sent to an enclosure operating at a lower pressure than the first phase separator. which can be a third phase separator 15.
  • third phase separator 15 is produced a liquid very rich in carbon dioxide 17 containing less impurities than the compressed flow rate in the compressor 1
  • a gas rich in at least one impurity 19 leaves the third phase separator 15 and can be heated in the exchange line 7.
  • the gas 25 of the first phase separator 9 is heated in the exchange line 7, compressed in the compressor 27 to form a compressed gas 29 at a pressure between 5 and 50 bar higher than the previous compression pressure.
  • the gas 29 cools in the exchange line 7 and is sent to a second phase separator 31.
  • the second liquid 33 of the second phase separator is expanded in a valve 35 to the pressure of the chamber 15.
  • the gas 36 of the second phase separator 31 is heated in the exchange line 7, is expanded in a turbine 37 and leaves the apparatus as a gas 39.
  • the exchange line 7 and the phase separators 9, 15, 31 are located inside an insulated enclosure (not shown) to allow operation at a subambient temperature.
  • the cold behavior of the apparatus is ensured by a refrigeration cycle 23 involving three compressors for compressing a cycle gas at three pressures, the cycle gas cooling and heating in the exchange line. Other methods of producing cold can be considered.
  • Figure 2 differs from Figure 1 in that it shows a means for preventing solidification of carbon dioxide.
  • the second liquid 33 leaving the second phase separator 31, operating at the highest pressure that the first phase separator, is heated in the exchange line 7 and leaves it at a temperature hotter than the cold end. of the exchange line (indicated by dashed lines, to show that the second heated liquid 33 does not cool in the exchanger).
  • the second phase separator 31 may be disposed at a height H above the inlet of the second liquid in the exchange line 7 to ensure that the pressure of the liquid 33 is sufficient to prevent its vaporization in the exchange line 7.
  • the liquid must be reheated in the exchange line 7 beforehand, in order to avoid going below -54.5 ° C. and to avoid the formation of gas in the process. relaxing, it requires the hydrostatic height corresponding to a height H between 2.9m and 44m depending on the composition of the liquid.
  • the trigger causes gas formation but it is not necessary to send this liquid to the exchange line 7 previously because the temperature is high enough to prevent the formation of solids.
  • Figure 3 differs from Figure 1 in that the liquid 33 of the second phase separator is not sent directly to the third phase separator 15 after expansion in the valve 35 but to the first phase separator.
  • the valve 35 relaxes the liquid 33 at a pressure intermediate that of the second separator 31 and that of the enclosure, thereby reducing the temperature drop.
  • the liquid sent from the first phase separator to the chamber 15 is in this case composed of the first liquid and the third liquid.
  • the third liquid is derived from the second liquid by separation in the first phase separator
  • the chamber operating at lower pressure than the first pressure may be the third phase separator 15 or else a distillation or washing column if the liquefied product 17 is to be purer.
  • a compressor 1 compresses a flow rich in carbon dioxide, containing at least 20% vol carbon dioxide, or at least 40% vol or at least 50% vol carbon dioxide, possibly at least 60% at least 70% vol of carbon dioxide and at least one light impurity which may be oxygen, nitrogen, argon, carbon monoxide, hydrogen, methane or more impurities.
  • the flow can come for example from an oxycombustion, a steel plant, a cement plant, a SMR ...
  • the flow After compression at a pressure between 8 and 40 bar a, the flow is cooled in a cooler, purified with water in the adsorption unit and then sent to cool in the exchange line 7 which may be constituted by a heat exchanger brazed aluminum plates and fins.
  • the cooled and partially condensed flow is sent to a first phase separator 9.
  • the first liquid 11 of the first phase separator 9 is expanded in a valve 13 and then sent to an enclosure 15 operating at a lower pressure than the first phase separator. This chamber being a distillation column.
  • distillation column 15 In the distillation column 15 is produced a liquid very rich in carbon dioxide 17 containing less impurities than the compressed flow rate in the compressor 1
  • a gas (not shown) rich in at least one impurity leaves the head of the column 15 and can heat up in the exchange line 7.
  • the gas 25 of the first phase separator 9 is heated in the exchange line 7, compressed in the compressor 27 to form a compressed gas 29 at a pressure between 5 and 50 bar higher than the previous compression pressure.
  • the gas 29 cools in the exchange line 7 and is sent to a second phase separator 31.
  • the second liquid 33 of the second phase separator is expanded in a valve 35 to the pressure of the column 15.
  • the gas 36 of the second phase separator 31 se heats up in the exchange line 7, is expanded in at least one turbine 37 and leaves the apparatus as gas.
  • the exchange line 7, the column 15 and the phase separators 9, 31 are located inside an insulated enclosure (not shown) to allow operation at a subambient temperature.
  • the cold behavior of the apparatus is provided by vaporization of the liquid 17 of the column 15 at three different pressures.
  • the vaporized liquid is then compressed in a compressor 116 and serves as product 118.
  • Other methods of producing cold can be envisaged.

Abstract

In a method for purifying a flow rich in carbon dioxide and containing at least one impurity lighter than carbon dioxide, the flow is cooled in a heat exchanger (7) and partially condensed, the partially condensed flow is sent to a first phase separator (9) operating under a first pressure, a gas from the first phase separator is compressed and sent to a second phase separator (31) operating under a second pressure higher than the first pressure, a first liquid (11) is sent from the first phase separator to a housing (15) operating under a pressure lower than the first pressure, and a second liquid (33) is sent to the housing.

Description

Procédé et appareil de purification d'un débit riche en dioxyde de carbone  Process and apparatus for purifying a flow rich in carbon dioxide
La présente invention est relative à un procédé et à un appareil de purification d'un débit riche en dioxyde de carbone. The present invention relates to a method and apparatus for purifying a flow rich in carbon dioxide.
Un débit riche en dioxyde de carbone contient au moins 20% vol. de dioxyde de carbone, voire au moins 40% vol. de dioxyde de carbone, voire au moins 50% vol de dioxyde de carbone ou même au moins 60% vol. ou au moins 70% vol. de dioxyde carbone.  A flow rich in carbon dioxide contains at least 20% vol. carbon dioxide, or at least 40% vol. of carbon dioxide, or at least 50% vol of carbon dioxide or even at least 60% vol. or at least 70% vol. of carbon dioxide.
Dans un appareil de purification d'un débit riche en dioxyde de carbone, le débit est refroidi et partiellement condensé. La phase liquide ainsi formée est enrichie en dioxyde de carbone et la phase gazeuse est enrichie en au moins un composant plus léger pouvant être de l'oxygène, de l'azote, de l'argon, du monoxyde de carbone, de l'hydrogène, du méthane etc selon la composition du débit à purifier.  In a purification apparatus of a flow rich in carbon dioxide, the flow is cooled and partially condensed. The liquid phase thus formed is enriched in carbon dioxide and the gaseous phase is enriched in at least one lighter component that can be oxygen, nitrogen, argon, carbon monoxide, hydrogen , methane etc. according to the composition of the flow to be purified.
Un appareil de purification d'un débit riche en dioxyde de carbone connu de A purification apparatus of a flow rich in carbon dioxide known from
WO-A-20090007937 comprend plusieurs séparateurs de phase, dont deux connectés en série. WO-A-20090007937 comprises a plurality of phase separators, two of which are connected in series.
Selon l'invention, l'appareil peut comprendre au moins deux séparateurs de phases opérant à des pressions différentes pour améliorer l'efficacité de la séparation.  According to the invention, the apparatus may comprise at least two phase separators operating at different pressures to improve the efficiency of the separation.
Selon un objet de l'invention, il est prévu un procédé de purification d'un débit riche en dioxyde de carbone et contenant au moins une impureté plus légère que le dioxyde de carbone dans lequel :  According to one object of the invention, there is provided a process for purifying a flow rich in carbon dioxide and containing at least one lighter impurity than carbon dioxide in which:
i) le débit est refroidi dans un échangeur de chaleur et partiellement condensé ii) le débit partiellement condensé est envoyé à un premier séparateur de phases opérant à une première pression  i) the flow is cooled in a heat exchanger and partially condensed ii) the partially condensed flow is sent to a first phase separator operating at a first pressure
iii) un gaz du premier séparateur de phases est réchauffé, comprimé, refroidi et envoyé à un deuxième séparateur de phases opérant à une deuxième pression supérieure à la première pression  iii) a gas of the first phase separator is heated, compressed, cooled and sent to a second phase separator operating at a second pressure greater than the first pressure
iv) un premier liquide est détendu et envoyé du premier séparateur de phases à une enceinte opérant à une pression inférieure à la première pression, v) un deuxième liquide provenant du deuxième séparateur de phases ou un troisième liquide dérivé du deuxième liquide est détendu et envoyé à l'enceinte et iv) a first liquid is expanded and sent from the first phase separator to an enclosure operating at a pressure lower than the first pressure, v) a second liquid from the second phase separator or a third liquid derived from the second liquid is expanded and sent to the enclosure and
vi) un liquide purifié riche en dioxyde de carbone sort de l'enceinte.  vi) a purified liquid rich in carbon dioxide leaves the enclosure.
Le liquide envoyé du premier séparateur de phases à l'enceinte peut être composé du premier liquide et du troisième liquide mélangés, comme illustré pour la Figure 3. Le troisième liquide est dérivé du deuxième liquide par séparation dans le premier séparateur de phases.  The liquid sent from the first phase separator to the chamber may be composed of the first liquid and the third liquid mixed, as illustrated in FIG. 3. The third liquid is derived from the second liquid by separation in the first phase separator.
Selon d'autres caractéristiques facultatives :  According to other optional features:
- le deuxième liquide est réchauffé, éventuellement dans l'échangeur de chaleur, puis détendu dans une vanne jusqu'à la pression de l'enceinte et envoyé à l'enceinte.  - The second liquid is heated, possibly in the heat exchanger, and then expanded in a valve to the pressure of the chamber and sent to the enclosure.
- le deuxième séparateur de phases opère à une pression moins élevée que l'entrée du deuxième liquide dans l'échangeur, en raison d'une pression hydrostatique due à la position du deuxième séparateur de phases au-dessus de l'entrée du deuxième liquide dans l'échangeur.  the second phase separator operates at a lower pressure than the inlet of the second liquid in the exchanger, because of a hydrostatic pressure due to the position of the second phase separator above the inlet of the second liquid in the exchanger.
- le deuxième liquide est détendu d'abord à une pression intermédiaire entre la deuxième pression et la pression de l'enceinte et ensuite jusqu'à la pression de l'enceinte.  - The second liquid is first expanded to an intermediate pressure between the second pressure and the pressure of the chamber and then to the pressure of the chamber.
- le deuxième liquide est détendu jusqu'à la première pression, envoyé au premier séparateur de phases et le troisième liquide dérivé du deuxième liquide est envoyé du premier séparateur de phases à l'enceinte  the second liquid is expanded to the first pressure, sent to the first phase separator and the third liquid derived from the second liquid is sent from the first phase separator to the enclosure
- le procédé produit un produit final liquide riche en dioxyde de carbone  - the process produces a liquid end product rich in carbon dioxide
- l'enceinte est un séparateur de phases.  the enclosure is a phase separator.
- l'enceinte est une colonne de distillation ou de lavage.  the enclosure is a distillation or washing column.
-la température d'entrée du compresseur est substantiellement égale à la température de l'entrée du débit à refroidir dans l'échangeur de chaleur.  the inlet temperature of the compressor is substantially equal to the temperature of the inlet of the flow rate to be cooled in the heat exchanger.
Selon un autre objet de l'invention, il est prévu un appareil de purification d'un débit riche en dioxyde de carbone et contenant au moins une impureté plus légère que le dioxyde de carbone comprenant une enceinte, un compresseur, un premier séparateur de phases, un deuxième séparateur de phases, un échangeur de chaleur, une conduite pour envoyer le débit riche en dioxyde de carbone se refroidir dans l'échangeur de chaleur, une conduite pour amener le débit refroidi de l'échangeur au premier séparateur de phase, des moyens pour amener un gaz du premier séparateur de phases à l'échangeur de chaleur pour se réchauffer, des moyens pour amener ce gaz de l'échangeur de chaleur au compresseur, une conduite pour amener le gaz du compresseur à l'échangeur de chaleur, une conduite pour amener le gaz comprimé de l'échangeur de chaleur au deuxième séparateur de phases, une conduite pour amener un premier liquide du premier séparateur de phases à l'enceinte, une vanne pour détendre le premier liquide en amont de l'enceinte, une conduite pour sortir un liquide purifié riche en dioxyde de carbone de l'enceinte et According to another object of the invention, there is provided a device for purifying a flow rich in carbon dioxide and containing at least one lighter impurity than carbon dioxide comprising an enclosure, a compressor, a first phase separator a second phase separator, a heat exchanger, a pipe for sending the carbon dioxide-rich flow to be cooled in the heat exchanger, a pipe for bringing the cooled flow rate of the exchanger to the first phase separator, means for feeding a gas from the first phase separator to the heat exchanger for heating, means for supplying this gas from the heat exchanger to the compressor, a pipe for supplying the compressor gas to the heat exchanger, a pipe for bringing the compressed gas from the heat exchanger to the second phase separator , a pipe for bringing a first liquid of the first phase separator to the enclosure, a valve for expanding the first liquid upstream of the enclosure, a pipe for discharging a purified liquid rich in carbon dioxide from the enclosure and
i) des moyens pour soutirer un deuxième liquide du deuxième séparateur de phases et pour amener le deuxième liquide à l'enceinte et une vanne pour détendre le deuxième liquide en amont de l'enceinte ou  i) means for withdrawing a second liquid from the second phase separator and for bringing the second liquid to the enclosure and a valve for expanding the second liquid upstream of the enclosure or
ii)une conduite pour soutirer le deuxième liquide du deuxième séparateur de phases et pour l'envoyer au premier séparateur de phases, une conduite pour amener un troisième liquide dérivé du deuxième liquide du premier séparateur de phases à l'enceinte et une vanne pour détendre le troisième liquide en amont de l'enceinte.  ii) a pipe for withdrawing the second liquid from the second phase separator and for sending it to the first phase separator, a pipe for bringing a third liquid derived from the second liquid of the first phase separator to the enclosure and a valve for relaxing the third liquid upstream of the enclosure.
Selon d'autres caractéristiques facultatives :  According to other optional features:
- les moyens pour soutirer le deuxième liquide du deuxième séparateur de phases et pour amener le deuxième liquide à l'enceinte sont constitués par une conduite reliée à un point d'entrée de l'échangeur et au deuxième séparateur de phases et une conduite reliée à un point intermédiaire de l'échangeur et à l'enceinte.  the means for withdrawing the second liquid from the second phase separator and for bringing the second liquid to the chamber are constituted by a pipe connected to an inlet point of the exchanger and to the second phase separator and a pipe connected to an intermediate point of the exchanger and the enclosure.
- le point d'entrée de l'échangeur est en dessous du point de soutirage du deuxième liquide du deuxième séparateur de phases.  the point of entry of the exchanger is below the point of withdrawal of the second liquid from the second phase separator.
- l'appareil comprend des moyens pour détendre le deuxième liquide à une pression intermédiaire inférieure à la pression d'opération du deuxième séparateur de phases et des moyens pour détendre le deuxième liquide ou un troisième liquide dérivé du deuxième liquide à la pression de l'enceinte.  the apparatus comprises means for expanding the second liquid at an intermediate pressure lower than the operating pressure of the second phase separator and means for expanding the second liquid or a third liquid derived from the second liquid at the pressure of the second pregnant.
- l'appareil comprend des moyens reliant le deuxième séparateur de phases au premier séparateur de phases pour permettre le passage de liquide.  - The apparatus comprises means connecting the second phase separator to the first phase separator to allow the passage of liquid.
- l'enceinte est une colonne de distillation ou de lavage.  the enclosure is a distillation or washing column.
- l'enceinte est un troisième pot séparateur.  - the enclosure is a third separator pot.
Le gaz d'un premier séparateur de phase peut être comprimé à une pression plus élevée et recondensé, éventuellement à la même température. Quand le dioxyde de carbone est requis à haute pureté, (plus que 98% vol) une colonne de distillation peut être nécessaire. Dans ce cas, tous les débits liquides provenant des séparateurs de phases sont détendus et amenés vers un séparateur de phases ou la colonne de distillation. Dans ce cas, lors de la détente du débit à la plus haute pression, il peut être souhaitable de fonctionner à une température proche de la température de solidification afin d'augmenter le rendement de dioxyde de carbone pur. Le liquide qui se refroidit lors de la détente peut alors solidifier. Même si la pression partielle est telle que le dioxyde de carbone ne solidifie pas, la température atteinte pourrait être trop basse pour les autres fluides présents dans le séparateur ou la colonne de distillation, ainsi, ce serait le mélange dans le séparateur ou la colonne qui pourrait geler partiellement. Alternativement une canalisation de liquide installée dans la boîte froide proche d'une canalisation de dioxyde de carbone pourrait geler. The gas of a first phase separator can be compressed to a higher pressure and recondensed, possibly at the same temperature. When carbon dioxide is required at high purity, (more than 98% vol) a distillation column may be needed. In this case, all liquid flows from the phase separators are expanded and fed to a phase separator or distillation column. In this case, during the expansion of the flow at the highest pressure, it may be desirable to operate at a temperature close to the solidification temperature in order to increase the yield of pure carbon dioxide. The liquid that cools during relaxation can then solidify. Even if the partial pressure is such that the carbon dioxide does not solidify, the temperature reached could be too low for the other fluids present in the separator or the distillation column, thus, it would be the mixture in the separator or the column which could freeze partially. Alternatively a liquid line installed in the cold box near a carbon dioxide line could freeze.
Le risque principal n'est pas tellement la solidification complète des liquides riches en dioxyde de carbone mais plutôt la formation d'aiguilles de dioxyde de carbone qui pourrait abîmer des canalisations (surtout dans les coudes) et l'instrumentation (vannes, sondes ....).  The main risk is not so much the complete solidification of the carbon dioxide-rich liquids but rather the formation of carbon dioxide needles which could damage the pipes (especially in the elbows) and the instrumentation (valves, probes, etc.). ..).
La solution de base est d'éviter de trop refroidir le débit à plus haute pression de sorte que la phase liquide puisse être détendue sans risque.  The basic solution is to avoid overheating the flow at higher pressure so that the liquid phase can be relaxed without risk.
Cette approche réduit le rendement en dioxyde de carbone du procédé car elle réduit la pression et la température d'une condensation partielle.  This approach reduces the carbon dioxide yield of the process as it reduces the pressure and temperature of a partial condensation.
Une solution est de chauffer légèrement au moins un liquide à plus haute pression en amont de la détente de sorte qu'il reste au-dessus du point de solidification. Cette approche complique l'échangeur de chaleur qui refroidit le liquide.  One solution is to slightly heat at least one higher pressure liquid upstream of the expansion so that it remains above the solidification point. This approach complicates the heat exchanger that cools the liquid.
Dans ce cas, il est envisagé d'installer les séparateurs de phases et l'échangeur de chaleur de telle sorte qu'il y a suffisamment de hauteur hydrostatique pour éviter la vaporisation du liquide. Si le liquide du séparateur est chauffé, même un peu, à la même pression, il commencera tout de suite à vaporiser. Une pression plus élevée est requise pour que le liquide reste liquide à la température plus élevée.  In this case, it is envisaged to install the phase separators and the heat exchanger so that there is sufficient hydrostatic head to prevent the vaporization of the liquid. If the liquid of the separator is heated, even a little, at the same pressure, it will begin to vaporize immediately. Higher pressure is required for the liquid to remain liquid at the higher temperature.
Encore une autre solution est de détendre au moins un des liquides à la plus haute pression par étapes. Une possibilité est de détendre le liquide à plus haute pression dans un séparateur de phases intermédiaire dont le liquide est envoyé à la colonne. Un avantage de cette solution est qu'elle réduit le nombre de conduites dans la boîte froide et le nombre de connexions à la colonne et le nombre de connexions sur l'échangeur principal et enfin les contraintes d'arrangement liées à des besoins de hauteur hydrostatique. Yet another solution is to relax at least one of the liquids at the highest pressure in stages. One possibility is to relax the liquid at higher pressure in an intermediate phase separator whose liquid is sent to the column. An advantage of this solution is that it reduces the number of pipes in the cold box and the number of connections to the column and the number of connections on the main exchanger and finally the arrangement constraints related to hydrostatic head requirements. .
L'invention sera décrite en plus de détail en se référant aux figures. Les figures 1 à 4 montrent des appareils selon l'invention.  The invention will be described in more detail with reference to the figures. Figures 1 to 4 show apparatus according to the invention.
Dans la Figure 1 , un compresseur 1 comprime un débit riche en dioxyde de carbone, contenant au moins 20% vol de dioxyde de carbone, voire au moins 40% vol de dioxyde de carbone, éventuellement au moins 60% vol de dioxyde de carbone et au moins une impureté légère pouvant être de l'oxygène, de l'azote, de l'argon, du monoxyde de carbone, de l'hydrogène, du méthane ou plusieurs de ces impuretés. Le débit peut provenir par exemple d'une oxycombustion, d'une aciérie, d'une cimenterie, d'un SMR...  In Figure 1, a compressor 1 compresses a flow rich in carbon dioxide, containing at least 20% vol carbon dioxide, or even at least 40% vol carbon dioxide, possibly at least 60% vol carbon dioxide and at least one light impurity which may be oxygen, nitrogen, argon, carbon monoxide, hydrogen, methane or several of these impurities. The flow can come for example from an oxycombustion, a steel plant, a cement plant, a SMR ...
Après la compression à une pression entre 8 et 40 bars a., le débit est refroidi dans le refroidisseur 4, épuré en eau dans l'unité d'adsorption 5 puis envoyé se refroidir dans la ligne d'échange 7 qui peut être constituée par un échangeur à plaques et à ailettes en aluminium bras é .  After compression at a pressure between 8 and 40 bar a, the flow is cooled in the cooler 4, purified with water in the adsorption unit 5 and then sent to cool in the exchange line 7 which can be constituted by a plate and fin heat exchanger aluminum arm é.
Le débit refroidi et partiellement condensé est envoyé à un premier séparateur de phases 9. Le premier liquide 1 1 du premier séparateur de phases 9 est détendu dans une vanne 13 puis envoyé à une enceinte opérant à plus basse pression que le premier séparateur de phases, pouvant être un troisième séparateur de phases 15.  The cooled and partially condensed flow rate is sent to a first phase separator 9. The first liquid 1 1 of the first phase separator 9 is expanded in a valve 13 and then sent to an enclosure operating at a lower pressure than the first phase separator. which can be a third phase separator 15.
En troisième séparateur de phases 15 est produit un liquide très riche en dioxyde de carbone 17 contenant moins d'impuretés que le débit comprimé dans le compresseur 1  In third phase separator 15 is produced a liquid very rich in carbon dioxide 17 containing less impurities than the compressed flow rate in the compressor 1
Un gaz riche en au moins une impureté 19 sort du troisième séparateur de phases 15 et peut se réchauffer dans la ligne d'échange 7.  A gas rich in at least one impurity 19 leaves the third phase separator 15 and can be heated in the exchange line 7.
Le gaz 25 du premier séparateur de phases 9 est réchauffé dans la ligne d'échange 7, comprimé dans le compresseur 27 pour former un gaz comprimé 29 à une pression entre 5 et 50 bars plus élevée que la précédente pression de compression. Le gaz 29 se refroidit dans la ligne d'échange 7 et est envoyé à un deuxième séparateur de phases 31. Le deuxième liquide 33 du deuxième séparateur de phases est détendu dans une vanne 35 jusqu'à la pression de l'enceinte 15. Le gaz 36 du deuxième séparateur de phases 31 se réchauffe dans la ligne d'échange 7, est détendu dans une turbine 37 et sort de l'appareil comme gaz 39. La ligne d'échange 7 et les séparateurs de phases 9,15, 31 se trouvent à l'intérieur d'une enceinte isolée (non-illustrée) pour permettre l'opération à une température subambiante. The gas 25 of the first phase separator 9 is heated in the exchange line 7, compressed in the compressor 27 to form a compressed gas 29 at a pressure between 5 and 50 bar higher than the previous compression pressure. The gas 29 cools in the exchange line 7 and is sent to a second phase separator 31. The second liquid 33 of the second phase separator is expanded in a valve 35 to the pressure of the chamber 15. The gas 36 of the second phase separator 31 is heated in the exchange line 7, is expanded in a turbine 37 and leaves the apparatus as a gas 39. The exchange line 7 and the phase separators 9, 15, 31 are located inside an insulated enclosure (not shown) to allow operation at a subambient temperature.
La tenue en froid de l'appareil est assurée par un cycle frigorifique 23 impliquant trois compresseurs pour comprimer un gaz de cycle à trois pressions, le gaz du cycle se refroidissant et se réchauffant dans la ligne d'échange. D'autres méthodes de production de froid peuvent être envisagées.  The cold behavior of the apparatus is ensured by a refrigeration cycle 23 involving three compressors for compressing a cycle gas at three pressures, the cycle gas cooling and heating in the exchange line. Other methods of producing cold can be considered.
La Figure 2 diffère de la Figure 1 en ce qu'elle montre un moyen pour éviter la solidification de dioxyde de carbone. Le deuxième liquide 33 sortant du deuxième séparateur de phases 31 , opérant à la pression la plus élevée que le premier séparateur de phases, est réchauffé dans la ligne d'échange 7 et sort de celle-ci à une température plus chaude que le bout froid de la ligne d'échange (indiqué par des lignes pointillées, pour montrer que le deuxième liquide 33 réchauffé ne se refroidit pas dans l'échangeur).  Figure 2 differs from Figure 1 in that it shows a means for preventing solidification of carbon dioxide. The second liquid 33 leaving the second phase separator 31, operating at the highest pressure that the first phase separator, is heated in the exchange line 7 and leaves it at a temperature hotter than the cold end. of the exchange line (indicated by dashed lines, to show that the second heated liquid 33 does not cool in the exchanger).
En addition, le deuxième séparateur de phases 31 peut être disposé à une hauteur H au-dessus de l'entrée du deuxième liquide dans la ligne d'échange 7 pour s'assurer que la pression du liquide 33 est suffisante pour empêcher sa vaporisation dans la ligne d'échange 7.  In addition, the second phase separator 31 may be disposed at a height H above the inlet of the second liquid in the exchange line 7 to ensure that the pressure of the liquid 33 is sufficient to prevent its vaporization in the exchange line 7.
Si la pression du liquide 33 est détendu dans la vanne 35 jusqu'à 10 bars abs, il faut réchauffer le liquide dans la ligne d'échange 7 auparavant, pour éviter de descendre sous - 54.5°C et pour éviter la formation de gaz en détendant, il faut de la hauteur hydrostatique correspondant à une hauteur H entre 2,9m et 44m selon la composition du liquide.  If the pressure of the liquid 33 is expanded in the valve 35 up to 10 bar abs, the liquid must be reheated in the exchange line 7 beforehand, in order to avoid going below -54.5 ° C. and to avoid the formation of gas in the process. relaxing, it requires the hydrostatic height corresponding to a height H between 2.9m and 44m depending on the composition of the liquid.
Si la pression du liquide du liquide 33 sortant de la vanne 35 est à 20 bars abs, la détente provoque une formation de gaz mais il n'est pas nécessaire d'envoyer ce liquide à la ligne d'échange 7 auparavant car la température est suffisamment élevée pour éviter la formation de solides.  If the liquid liquid 33 pressure exiting the valve 35 is at 20 bar abs, the trigger causes gas formation but it is not necessary to send this liquid to the exchange line 7 previously because the temperature is high enough to prevent the formation of solids.
La Figure 3 diffère de la Figure 1 en ce que le liquide 33 du deuxième séparateur de phases n'est pas envoyé directement au troisième séparateur de phases 15 après sa détente dans la vanne 35 mais au premier séparateur de phases. Ainsi la vanne 35 détend le liquide 33 à une pression intermédiaire entre celle du deuxième séparateur 31 et celle de l'enceinte, réduisant ainsi la chute de température. Le liquide envoyé du premier séparateur de phases à l'enceinte 15 est donc dans ce cas composé du premier liquide et du troisième liquide. Le troisième liquide est dérivé du deuxième liquide par séparation dans le premier séparateur de phases Figure 3 differs from Figure 1 in that the liquid 33 of the second phase separator is not sent directly to the third phase separator 15 after expansion in the valve 35 but to the first phase separator. Thus the valve 35 relaxes the liquid 33 at a pressure intermediate that of the second separator 31 and that of the enclosure, thereby reducing the temperature drop. The liquid sent from the first phase separator to the chamber 15 is in this case composed of the first liquid and the third liquid. The third liquid is derived from the second liquid by separation in the first phase separator
L'enceinte opérant à plus basse pression que la première pression peut être le troisième séparateur de phases 15 ou sinon une colonne de distillation ou de lavage si le produit liquéfié 17 doit être plus pur.  The chamber operating at lower pressure than the first pressure may be the third phase separator 15 or else a distillation or washing column if the liquefied product 17 is to be purer.
Dans la Figure 4, un compresseur 1 comprime un débit riche en dioxyde de carbone, contenant au moins 20% vol de dioxyde de carbone, voire au moins 40% vol ou au moins 50% vol de dioxyde de carbone, éventuellement au moins 60% vol ou au moins 70% vol de dioxyde de carbone et au moins une impureté légère pouvant être de l'oxygène, de l'azote, de l'argon, du monoxyde de carbone, de l'hydrogène, du méthane ou plusieurs de ces impuretés. Le débit peut provenir par exemple d'une oxycombustion, d'une aciérie, d'une cimenterie, d'un SMR...  In Figure 4, a compressor 1 compresses a flow rich in carbon dioxide, containing at least 20% vol carbon dioxide, or at least 40% vol or at least 50% vol carbon dioxide, possibly at least 60% at least 70% vol of carbon dioxide and at least one light impurity which may be oxygen, nitrogen, argon, carbon monoxide, hydrogen, methane or more impurities. The flow can come for example from an oxycombustion, a steel plant, a cement plant, a SMR ...
Après la compression à une pression entre 8 et 40 bars a., le débit est refroidi dans un refroidisseur, épuré en eau dans l'unité d'adsorption puis envoyé se refroidir dans la ligne d'échange 7 qui peut être constituée par un échangeur à plaques et à ailettes en aluminium brasé.  After compression at a pressure between 8 and 40 bar a, the flow is cooled in a cooler, purified with water in the adsorption unit and then sent to cool in the exchange line 7 which may be constituted by a heat exchanger brazed aluminum plates and fins.
Le débit refroidi et partiellement condensé est envoyé à un premier séparateur de phases 9. Le premier liquide 11 du premier séparateur de phases 9 est détendu dans une vanne 13 puis envoyé à une enceinte 15 opérant à plus basse pression que le premier séparateur de phases, cette enceinte étant une colonne de distillation.  The cooled and partially condensed flow is sent to a first phase separator 9. The first liquid 11 of the first phase separator 9 is expanded in a valve 13 and then sent to an enclosure 15 operating at a lower pressure than the first phase separator. this chamber being a distillation column.
Dans la colonne de distillation 15 est produit un liquide très riche en dioxyde de carbone 17 contenant moins d'impuretés que le débit comprimé dans le compresseur 1 In the distillation column 15 is produced a liquid very rich in carbon dioxide 17 containing less impurities than the compressed flow rate in the compressor 1
Un gaz (non-illustré) riche en au moins une impureté sort de la tête de la colonne 15 et peut se réchauffer dans la ligne d'échange 7. A gas (not shown) rich in at least one impurity leaves the head of the column 15 and can heat up in the exchange line 7.
Le gaz 25 du premier séparateur de phases 9 est réchauffé dans la ligne d'échange 7, comprimé dans le compresseur 27 pour former un gaz comprimé 29 à une pression entre 5 et 50 bars plus élevée que la précédente pression de compression. Le gaz 29 se refroidit dans la ligne d'échange 7 et est envoyé à un deuxième séparateur de phases 31. Le deuxième liquide 33 du deuxième séparateur de phases est détendu dans une vanne 35 jusqu'à la pression de la colonne 15. Le gaz 36 du deuxième séparateur de phases 31 se réchauffe dans la ligne d'échange 7, est détendu dans au moins une turbine 37 et sort de l'appareil comme gaz. The gas 25 of the first phase separator 9 is heated in the exchange line 7, compressed in the compressor 27 to form a compressed gas 29 at a pressure between 5 and 50 bar higher than the previous compression pressure. The gas 29 cools in the exchange line 7 and is sent to a second phase separator 31. The second liquid 33 of the second phase separator is expanded in a valve 35 to the pressure of the column 15. The gas 36 of the second phase separator 31 se heats up in the exchange line 7, is expanded in at least one turbine 37 and leaves the apparatus as gas.
La ligne d'échange 7, la colonne 15 et les séparateurs de phases 9, 31 se trouvent à l' intérieur d'une enceinte isolée (non-illustrée) pour permettre l'opération à une température subambiante.  The exchange line 7, the column 15 and the phase separators 9, 31 are located inside an insulated enclosure (not shown) to allow operation at a subambient temperature.
La tenue en froid de l'appareil est assurée par vaporisation du liquide 17 de la colonne 15 à trois pressions différentes. Le liquide vaporisé est ensuite comprimé dans un compresseur 1 16 et sert de produit 118. D'autres méthodes de production de froid peuvent être envisagées.  The cold behavior of the apparatus is provided by vaporization of the liquid 17 of the column 15 at three different pressures. The vaporized liquid is then compressed in a compressor 116 and serves as product 118. Other methods of producing cold can be envisaged.

Claims

Revendications claims
1. Procédé de purification d'un débit riche en dioxyde de carbone et contenant au moins une impureté plus légère que le dioxyde de carbone dans lequel : A process for purifying a flow rich in carbon dioxide and containing at least one lighter impurity than carbon dioxide in which:
i) le débit est refroidi dans un échangeur de chaleur (7) et partiellement condensé ii) le débit partiellement condensé est envoyé à un premier séparateur de phases (9) opérant à une première pression  i) the flow is cooled in a heat exchanger (7) and partially condensed ii) the partially condensed flow is sent to a first phase separator (9) operating at a first pressure
iii) un gaz du premier séparateur de phases est réchauffé, comprimé, refroidi et envoyé à un deuxième séparateur de phases (31) opérant à une deuxième pression supérieure à la première pression  iii) a gas of the first phase separator is heated, compressed, cooled and sent to a second phase separator (31) operating at a second pressure greater than the first pressure
iv) un premier liquide (1 1) est détendu et envoyé du premier séparateur de phases à une enceinte (15) opérant à une pression inférieure à la première pression,  iv) a first liquid (1 1) is expanded and sent from the first phase separator to an enclosure (15) operating at a pressure lower than the first pressure,
v) un deuxième liquide (33) provenant du deuxième séparateur de phases ou un troisième liquide (1 1) dérivé du deuxième liquide est détendu et envoyé à l'enceinte et vi) un liquide (17) purifié riche en dioxyde de carbone sort de l'enceinte.  v) a second liquid (33) from the second phase separator or a third liquid (1 1) derived from the second liquid is expanded and sent to the chamber and vi) a purified liquid (17) rich in carbon dioxide comes out of the enclosure.
2. Procédé selon la revendication 1 dans lequel le deuxième liquide (33) est réchauffé, éventuellement dans l'échangeur de chaleur (7), puis détendu dans une vanne (35) jusqu'à la pression de l'enceinte (15) et envoyé à l'enceinte. 2. Method according to claim 1 wherein the second liquid (33) is heated, optionally in the heat exchanger (7), and then expanded in a valve (35) to the pressure of the enclosure (15) and sent to the enclosure.
3. Procédé selon la revendication 2 dans lequel le deuxième séparateur de phases (31) opère à une pression moins élevée que l'entrée du deuxième liquide (33) dans l'échangeur (7), en raison d'une pression hydrostatique due à la position du deuxième séparateur de phases au-dessus de l'entrée du deuxième liquide dans l'échangeur. 3. Method according to claim 2 wherein the second phase separator (31) operates at a lower pressure than the inlet of the second liquid (33) in the exchanger (7), due to a hydrostatic pressure due to the position of the second phase separator above the inlet of the second liquid in the exchanger.
4. Procédé selon l'une des revendications précédentes dans lequel le deuxième liquide (33) est détendu d'abord à une pression intermédiaire entre la deuxième pression et la pression de l'enceinte (15) et ensuite jusqu'à la pression de l'enceinte. 4. Method according to one of the preceding claims wherein the second liquid (33) is first expanded to an intermediate pressure between the second pressure and the pressure of the chamber (15) and then up to the pressure of the 'pregnant.
5. Procédé selon la revendication 4 dans lequel le deuxième liquide est détendu jusqu'à la première pression, envoyé au premier séparateur de phases (9) et le troisième liquide dérivé du deuxième liquide (1 1) est envoyé du premier séparateur de phases à l'enceinte (15). 5. Method according to claim 4 wherein the second liquid is expanded to the first pressure, sent to the first phase separator (9) and the third liquid derived from the second liquid (1 1) is sent from the first phase separator to the enclosure (15).
6. Procédé selon l'une des revendications précédentes dans lequel l'enceinte (15) est un séparateur de phases. 6. Method according to one of the preceding claims wherein the enclosure (15) is a phase separator.
7. Procédé selon l'une des revendications précédentes dans lequel l'enceinte (15) est une colonne de distillation ou de lavage. 7. Method according to one of the preceding claims wherein the enclosure (15) is a distillation column or washing.
8. Procédé selon l'une des revendications précédentes dans lequel la température d'entrée du compresseur (27) est substantiellement égale à la température de l'entrée du débit à refroidir dans l'échangeur de chaleur. 8. Method according to one of the preceding claims wherein the inlet temperature of the compressor (27) is substantially equal to the temperature of the flow inlet to be cooled in the heat exchanger.
9. Appareil de purification d'un débit riche en dioxyde de carbone et contenant au moins une impureté plus légère que le dioxyde de carbone comprenant une enceinte (15), un compresseur (27), un premier séparateur de phases (9), un deuxième séparateur de phases (31), un échangeur de chaleur (7), une conduite pour envoyer le débit riche en dioxyde de carbone se refroidir dans l'échangeur de chaleur, une conduite pour amener le débit refroidi de l'échangeur au premier séparateur de phase, des moyens pour amener un gaz du premier séparateur de phases à l'échangeur de chaleur pour se réchauffer, des moyens pour amener ce gaz de l'échangeur de chaleur au compresseur, une conduite pour amener le gaz comprimé du compresseur à l'échangeur de chaleur, une conduite pour amener le gaz comprimé de l'échangeur de chaleur au deuxième séparateur de phases, une conduite pour amener un premier liquide du premier séparateur de phases à l'enceinte, une vanne pour détendre le premier liquide en amont de l'enceinte une conduite pour sortir un liquide purifié riche en dioxyde de carbone de l'enceinte et Apparatus for purifying a flow rich in carbon dioxide and containing at least one lighter impurity than carbon dioxide comprising an enclosure (15), a compressor (27), a first phase separator (9), a second phase separator (31), a heat exchanger (7), a pipe for sending the carbon dioxide rich flow to be cooled in the heat exchanger, a pipe for bringing the cooled flow of the exchanger to the first separator phase, means for supplying a gas from the first phase separator to the heat exchanger for heating, means for supplying this gas from the heat exchanger to the compressor, a line for supplying compressed gas from the compressor to the compressor. heat exchanger, a pipe for supplying the compressed gas from the heat exchanger to the second phase separator, a pipe for supplying a first liquid of the first phase separator to the chamber, a valve for relieving pressure. first fluid upstream of the enclosure a pipe for discharging a purified liquid rich in carbon dioxide from the enclosure and
i) des moyens pour soutirer un deuxième liquide du deuxième séparateur de phases et pour amener le deuxième liquide à l'enceinte et une vanne pour détendre le deuxième liquide en amont de l'enceinte ou ii) une conduite pour soutirer le deuxième liquide du deuxième séparateur de phases et pour l'envoyer au premier séparateur de phases, une conduite pour amener un troisième liquide dérivé du deuxième liquide du premier séparateur de phases à l'enceinte et une vanne pour détendre le troisième liquide en amont de l'enceinte. i) means for withdrawing a second liquid from the second phase separator and for bringing the second liquid to the enclosure and a valve for expanding the second liquid upstream of the enclosure or ii) a pipe for withdrawing the second liquid from the second phase separator and for sending it to the first phase separator, a pipe for bringing a third liquid derived from the second liquid of the first phase separator to the enclosure and a valve for relaxing the third liquid upstream of the enclosure.
10. Appareil selon la revendication 9 dans lequel les moyens pour soutirer le deuxième liquide du deuxième séparateur de phases (31) et pour amener le deuxième liquide à l'enceinte (15) sont constitués par une conduite reliée à un point d'entrée de l'échangeur (7) et au deuxième séparateur de phases et une conduite reliée à un point intermédiaire de l'échangeur et à l'enceinte. 10. Apparatus according to claim 9 wherein the means for withdrawing the second liquid from the second phase separator (31) and to bring the second liquid to the enclosure (15) are constituted by a pipe connected to an entry point of the exchanger (7) and the second phase separator and a pipe connected to an intermediate point of the exchanger and to the enclosure.
11. Appareil selon la revendication 10 dans lequel le point d'entrée de l'échangeur est en dessous du point de soutirage du deuxième liquide du deuxième séparateur de phases (31). 11. Apparatus according to claim 10 wherein the point of entry of the exchanger is below the point of withdrawal of the second liquid of the second phase separator (31).
12. Appareil selon la revendication 9 à 11 comprenant des moyens pour détendre le deuxième liquide à une pression intermédiaire inférieure à la pression d'opération du deuxième séparateur de phases (31) et des moyens pour détendre le deuxième liquide ou un troisième liquide dérivé du deuxième liquide à la pression de l'enceinte (15). Apparatus according to claim 9 to 11 comprising means for expanding the second liquid to an intermediate pressure lower than the operating pressure of the second phase separator (31) and means for expanding the second liquid or a third liquid derived from the second liquid at the pressure of the enclosure (15).
13. Appareil selon la revendication 12 comprenant des moyens reliant le deuxième séparateur de phases (31) au premier séparateur de phases (9) pour permettre le passage de liquide. 13. Apparatus according to claim 12 including means connecting the second phase separator (31) to the first phase separator (9) to allow the passage of liquid.
14. Appareil selon l'une des revendications 9 à 13 dans lequel l'enceinte (15) est une colonne de distillation ou de lavage. 14. Apparatus according to one of claims 9 to 13 wherein the enclosure (15) is a distillation column or washing.
EP11794550.1A 2010-11-16 2011-11-14 Method and appliance for purifying a flow rich in carbon dioxide Withdrawn EP2641043A2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1059389A FR2967485B1 (en) 2010-11-16 2010-11-16 GAS STREAM PURIFICATION SYSTEM COMPRISING AT LEAST 50% CO2, WITH INTEGRATED COMPRESSION FUNCTIONS.
FR1156755A FR2974361A1 (en) 2011-07-25 2011-07-25 Purifying a flow that is rich in carbon dioxide and contains impurity lighter than carbon dioxide, comprises cooling the flow in heat exchanger and partially condensing it, and sending condensed flow to first phase separator
PCT/FR2011/052631 WO2012066221A2 (en) 2010-11-16 2011-11-14 Method and appliance for purifying a flow rich in carbon dioxide

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EP2641043A2 true EP2641043A2 (en) 2013-09-25

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EP (1) EP2641043A2 (en)
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EP1197717A1 (en) 2000-10-12 2002-04-17 Linde Aktiengesellschaft Process and apparatus for air separation
FR2872890A1 (en) 2005-08-08 2006-01-13 Air Liquide Integrated process for adsorption and cryogenic separation for the production of carbon dioxide from sources containing low percentages of carbon dioxide
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US7819951B2 (en) 2007-01-23 2010-10-26 Air Products And Chemicals, Inc. Purification of carbon dioxide
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CN103492825A (en) 2014-01-01
US20130233171A1 (en) 2013-09-12
US9393515B2 (en) 2016-07-19
WO2012066221A2 (en) 2012-05-24
CN103492825B (en) 2015-09-09
WO2012066221A3 (en) 2013-10-03

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