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.

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

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• 2011
  • 2011-11-14 EP EP11794550.1A patent/EP2641043A2/de not_active Withdrawn
  • 2011-11-14 WO PCT/FR2011/052631 patent/WO2012066221A2/fr active Application Filing
  • 2011-11-14 US US13/885,849 patent/US9393515B2/en not_active Expired - Fee Related
  • 2011-11-14 CN CN201180055121.0A patent/CN103492825B/zh active Active

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