US20140208798A1 - Apparatus and Integrated Process for Separating a Mixture of Carbon Dioxide and at Least One Other Gas and for Separating Air by Cryogenic Distillation - Google Patents

Apparatus and Integrated Process for Separating a Mixture of Carbon Dioxide and at Least One Other Gas and for Separating Air by Cryogenic Distillation Download PDF

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US20140208798A1
US20140208798A1 US14/122,255 US201214122255A US2014208798A1 US 20140208798 A1 US20140208798 A1 US 20140208798A1 US 201214122255 A US201214122255 A US 201214122255A US 2014208798 A1 US2014208798 A1 US 2014208798A1
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Prior art keywords
water
air
tower
carbon dioxide
separation unit
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US14/122,255
Inventor
Marie Cognard
Arthur Darde
Benoit Davidian
Richard Dubettier-Grenier
Frederick Lockwood
Christophe Szamlewski
Xavier Traversac
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Assigned to L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: DAVIDIAN, BENOIT, DUBETTIER-GRENIER, RICHARD, LOCKWOOD, FREDERICK, SZAMLEWSKI, CHRISTOPHE, DARDE, ARTHUR, COGNARD, MARIE, TRAVERSAC, XAVIER
Publication of US20140208798A1 publication Critical patent/US20140208798A1/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • 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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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    • 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
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/102—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2257/00—Components to be removed
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    • B01D2257/108—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/502—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
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    • B01D2257/7025—Methane
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust gas
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
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    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • 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

  • This invention relates to an apparatus and integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation.
  • It relates in particular to an apparatus and integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation, with water cooling intended to cool the mixture and/or the air upstream of the separation.
  • Compression and purification apparatuses treating supplies that are rich in CO 2 (more than 35% volume on a dry basis, preferably more than 70%) produce in essence a flow with less CO 2 content than the supply and containing the gases that will have been extracted from the product.
  • the purification of the CO 2 can take place thanks to one or several partial condensation(s) or by membrane separation or any other process (adsorption, cryo-condensation, etc.).
  • the flow of impure gas is a dry product. This will not be the case for a separation by scrubbing with amines for example, wherein the two products of the separation (the CO 2 and the residual gases) will be wet.
  • CO 2 treatment units include a step of drying the gases treated. This can be drying via adsorption. A dry gas must then be used to regenerate the adsorbent when it is saturated with water.
  • the state of the art provides as such to use the gases vaporised from the storage of CO 2 or residual gases, at high or low pressure.
  • EP-A-0503190 discloses a water cooling system for an apparatus for separating a mixture of carbon dioxide, oxygen and nitrogen wherein a water cooling tower is supplied with expanded nitrogen coming from an apparatus for separating air and water, with the cooled water then being used to cool the mixture to be separated. Before it is sent to the tower, the nitrogen is sent to the top condenser of a distillation column and then to the cooling exchanger of the mixture to be separated. This complicated arrangement requires the presence of a turbine so that the nitrogen has enough refrigeration to supply the required cold. None makes it possible to think that this cold would be sufficient to cool both the water for the apparatus for separating the mixture and the apparatus for separating air.
  • the invention proposes, according to certain alternatives, another use for the dry residual gases. They can as such be saturated with water in a tower that operates by direct contact, making it possible as such to lower the temperature of the unevaporated water and produce chilled water.
  • the method is commonly used on the apparatuses for separating air in “water-nitrogen towers” in order to cool the water by heat exchange and evaporation with the cold nitrogen coming from the apparatus for separating air.
  • a first portion of the cooling of the water could be carried out in a “non-condensable water” tower, with the first portion of the cooling being supplemented by a second portion of cooling in a refrigeration unit.
  • an apparatus for separating air having a water cooling tower located in the vicinity of an apparatus for separating a mixture of carbon dioxide and at least one other gas, using the water-nitrogen tower in order to produce cold water for the two apparatuses and also possibly saturating therein the incondensable items (which will then share the venting of the nitrogen) will allow for genuine gains in investment in relation to using two independent towers.
  • the CO 2 contained in the incondensable items must be prevented at all cost from rising back up to the apparatus for separating air via the line for transferring the dry nitrogen to the water-nitrogen tower. In normal operation as in the case of degraded mode, there is a real risk of introducing CO 2 into the apparatus for separating air and of clogging it when the CO 2 has frozen.
  • a precautionary measure which is claimed as inventive also, consists in expanding the incondensable items sufficiently far from the tower so that over a distance that will be deemed as reasonable, the pressure in the supply pipe of the tower is lower for the line of incondensable items than for the line of nitrogen.
  • the process consists in cooling the water by using nitrogen from an ASU and possibly at least one gas coming from a unit for separating a mixture of CO 2 and at least one other gas, which can for example be nitrogen, oxygen, argon, carbon monoxide, hydrogen, methane, NO 2 or a mixture of at least two of these gases.
  • an integrated apparatus for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation comprising a unit for separating a gaseous mixture comprising carbon dioxide at and least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and a unit for separating air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that it comprises a water cooling tower that operates by direct contact as well as a line for sending water to the top of the tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the tower, a cooled water line for withdrawing cooled water from the tower and means for cooling the air upstream of the air separation unit, the cooled water line being connected to means for cooling the air upstream of the air separation unit and to the inlet and/or to the outlet of the unit for separating the gaseous mixture.
  • an integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation comprising a unit for separating a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and a unit for separating air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that water is cooled in a water cooling tower that operates by direct contact with the nitrogen-enriched gas stream, the air intended for the air separation unit is cooled with the cooled water in the cooling tower and the gaseous mixture intended for the unit for separating the gaseous mixture and/or a product from the unit for separating the gaseous mixture is cooled using the cooled water coming from the cooling tower.
  • an integrated apparatus for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation
  • a unit for separating a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and an air separation unit by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that it comprises a water cooling tower that operates by direct contact as well as a line for sending water to the top of the tower, a line for sending carbon dioxide depleted gas to a lower level of the tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the tower, a cooled water line for withdrawing cooled water from the tower, means for cooling the air upstream of the air separation unit, the cooled water line being connected to the means for cooling the air upstream of the air separation unit.
  • An advantage of this invention is that it allows for the integration of production of cold water for apparatuses for separating with as the only connection between the two apparatuses a cooled water line, although a solution according to prior art requires a nitrogen line under pressure that connects the two apparatuses.
  • FIG. 1 shows an embodiment of the invention.
  • FIG. 2 shows an embodiment of the invention.
  • FIG. 3 shows an embodiment of the invention.
  • FIG. 4 shows an embodiment of the invention.
  • FIG. 1 shows an apparatus and an integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation according to the invention.
  • FIGS. 2 to 4 show the details of various water cooling towers used to cool the air upstream of the air separation by distillation in FIG. 1 , according to the invention.
  • a stream of air 1 is cooled in a pre-cooling unit P comprising an air scrubbing tower with water and a water cooling tower with nitrogen 17 .
  • This type of cooling is well known in the “Industrial Gas Handbook” by F. G. Kerry, page 112.
  • the air 3 cooled in the pre-cooling unit P is sent to an apparatus for separating air ASU wherein it is purified in order to remove the carbon dioxide and the moisture, cooled and separated in a system of columns in order to produce oxygen 5 and nitrogen 17 .
  • the oxygen 5 is sent to an oxy-fuel combustion boiler B also supplied with fuel 7 .
  • Fumes 9 coming from the oxy-fuel combustion unit B contain at least 40 mol. % of carbon dioxide on a dry basis, or even at least 60 mol. % of carbon dioxide, and at least one component chosen from the following list: nitrogen, oxygen, argon, hydrogen, carbon monoxide, methane or NO 2 .
  • the fumes are treated in a separating unit CPU.
  • the fumes 9 are cooled in a cooling unit R by heat exchange with cold water 15 .
  • the fumes are possibly compressed and then separated by phase separation and/or distillation in the unit CPU at a sub-ambient temperature.
  • the carbon dioxide depleted stream 13 can be a stream of nitrogen, oxygen, argon or NO 2 or a mixture of at least two of these gases.
  • the stream 13 exits the unit CPU at a temperature close to ambient temperature ( ⁇ 10° C.
  • the expanded gas 13 can be sent to pre-cooling.
  • the nitrogen 17 is sent directly from the apparatus for separating air ASU to the pre-cooling unit P without passing through another means of treatment, such as a turbine or an exchanger other than the air cooling exchanger associated with the apparatus for separating air ASU.
  • the pre-cooling unit produces cold water which is sent either to the unit R as a stream 15 or is used in the unit P or both.
  • FIG. 2 shows detail of the pre-cooling unit P.
  • This unit comprises a cooling tower 33 wherein the water 31 comes into direct contact with nitrogen 17 coming from the apparatus for separating air ASU.
  • the expanded gas 13 can be sent to the tower at a level higher than the inlet level of the nitrogen 17 , possibly separated from the inlet level of the nitrogen by a lining stage.
  • the nitrogen 17 comes from the apparatus ASU directly and arrives in the tower 33 without passing through the elements R or CPU.
  • the water cooling tower 33 is supplied at the top by a stream of water 31 at a temperature from 4° C. to 40° C.
  • the pressure of the stream 13 is slightly less than that of the stream 17 at the inlet in the tower 33 , thanks to the expansion in the valve V upstream of the tower, in order to prevent polluting the cooled water.
  • the gas 17 and possibly the gas 13 cool the water by direct contact and evaporation of a portion of the water in these dry gases and the mixture formed 39 exits at the top of the tower as venting.
  • the water heated in the unit CPU can be sent back to the unit P via the supply 21 .
  • the cooled water in the tank of the tower 33 is pumped by a pump 25 in order to be sent to the air cooling tower with water by the line 27 . Otherwise the cooled water can be sent to an exchanger with indirect contact in order to transfer refrigeration to the air intended for the distillation. A portion of this water 27 can also be used to provide refrigeration to the unit CPU, for example upstream of the desiccation unit.
  • This process may possibly not use a mechanical refrigeration unit such as a refrigeration unit.
  • the tower 33 will possibly be somewhat larger than that used solely for providing water for the air separation unit ASU.
  • a refrigeration unit 35 is used. In this way, instead of having a refrigeration unit for each of the units, a single refrigeration unit can cool the air separation unit ASU and the unit for separating the mixture containing carbon dioxide CPU.
  • FIG. 3 shows detail of the pre-cooling unit P.
  • This unit P comprises a cooling tower 33 wherein the water 31 comes into contact direct with nitrogen 17 coming from the apparatus for separating air ASU and an air cooling tower with water 133 .
  • the expanded gas 13 is possibly sent to the tower 33 at a level higher than the inlet level of the nitrogen 17 .
  • the nitrogen 17 comes from the apparatus ASU directly and arrives in the tower 33 without passing through the elements R or CPU.
  • the water cooling tower 33 is supplied at the top by a stream of water 31 at a temperature from 10° C. to 50° C.
  • the pressure of the stream 13 is slightly less than that of the stream 17 at the inlet in the tower 33 , thanks to the expansion in the valve V upstream of the tower.
  • the operating pressure of the tower 33 is substantially equal to the pressure at which the nitrogen 17 exits the apparatus for separating air ASU.
  • the gas 17 and possibly the gas 13 cool the water by direct contact and evaporation and the mixture formed 39 exits at the top of the tower as venting.
  • the cooled water in the tank of the tower 33 is pumped by a pump 25 in order to be sent to the top of the air cooling tower with water 133 as a stream 37 .
  • the air 1 intended for the distillation is cooled by being sent to the tank of the tower 133 .
  • the cooling water 21 is sent to an intermediate level of the tower 133 as a stream 121 and to the top of the tower 33 as a stream 31 .
  • the water cools the air by producing, at the top of the tower 133 , a stream of cooled air 3 which is sent for purification and then for distillation in the air separation unit ASU.
  • the heated water 221 is collected in the tank of the tower 133 and is recycled in the tower 133 after exterior refrigeration (by using air coolers, through exchange with cold water, etc.). It can also be considered that the water 221 is not recycled but returns, for example, to a river or a water network downstream.
  • the cooled water 23 collected in the tank of the tower 33 is pressurised by the pump 25 and a portion 15 is sent to the separation unit CPU.
  • the rest of the water is cooled by a refrigeration unit 35 in order to constitute the stream 37 sent to the top of the tower 133 .
  • FIG. 4 differs from FIG. 3 only in that all of the water coming from the pump 25 is cooled in the refrigeration unit before it is divided into two.
  • the cooled stream 37 is sent to the top of the tower 133 and the cooled stream 15 is sent to the unit CPU.
  • the cooled water 15 sent to the CPU can be used to cool the mixture to be separated or to cool a product from the separation.
  • the unit CPU does not necessarily operate at sub-ambient temperature.
  • the water heated in the unit CPU can be sent to the unit P via the supply 21 .
  • the apparatus for separating air ASU does not necessarily supply an oxy-fuel combustion unit, if present, with oxygen. It is sufficient for the apparatus for separating air ASU to be located relatively close to the unit CPU to allow for the integration between the two.
  • the gas can be sent to the cooling tower and the wet gas formed at the top of the tower can be used as a fuel, for example in a gas turbine.
  • “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.
  • Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
  • Optional or optionally means that the subsequently described event or circumstances may or may not occur.
  • the description includes instances where the event or circumstance occurs and instances where it does not occur.
  • Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.

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Abstract

An integrated apparatus for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation is provided. The apparatus includes a CO2 separation unit configured to separate the mixture, an air separation unit configured to separate air by cryogenic distillation, a water cooling tower that operates by direct contact, a line for sending water to the top of the tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the tower, a cooled water line for withdrawing cooled water from the tower and means for cooling the air upstream of the air separation unit, the cooled water line being connected to means for cooling the air upstream of the air separation unit and to the inlet and/or to the outlet of the unit for separating the gaseous mixture.

Description

    CROSS REFERENCE TO RELATED APPLICATIONS
  • This application is a §371 of International PCT Application PCT/FR2012/051203, filed May 29, 2012, which claims the benefit of FR1154754, filed May 31, 2011, both of which are herein incorporated by reference in their entireties.
    • TECHNICAL FIELD OF THE INVENTION
  • This invention relates to an apparatus and integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation.
  • It relates in particular to an apparatus and integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation, with water cooling intended to cool the mixture and/or the air upstream of the separation.
    • BACKGROUND
  • Compression and purification apparatuses treating supplies that are rich in CO2 (more than 35% volume on a dry basis, preferably more than 70%) produce in essence a flow with less CO2 content than the supply and containing the gases that will have been extracted from the product. The purification of the CO2 can take place thanks to one or several partial condensation(s) or by membrane separation or any other process (adsorption, cryo-condensation, etc.). In certain processes such as those mentioned, the flow of impure gas is a dry product. This will not be the case for a separation by scrubbing with amines for example, wherein the two products of the separation (the CO2 and the residual gases) will be wet.
  • Most CO2 treatment units include a step of drying the gases treated. This can be drying via adsorption. A dry gas must then be used to regenerate the adsorbent when it is saturated with water. The state of the art provides as such to use the gases vaporised from the storage of CO2 or residual gases, at high or low pressure.
  • It is known from EP-A-1712858 to use a carbon dioxide depleted gas to cool the water in a water cooling tower.
  • EP-A-0503190 discloses a water cooling system for an apparatus for separating a mixture of carbon dioxide, oxygen and nitrogen wherein a water cooling tower is supplied with expanded nitrogen coming from an apparatus for separating air and water, with the cooled water then being used to cool the mixture to be separated. Before it is sent to the tower, the nitrogen is sent to the top condenser of a distillation column and then to the cooling exchanger of the mixture to be separated. This complicated arrangement requires the presence of a turbine so that the nitrogen has enough refrigeration to supply the required cold. Nothing makes it possible to think that this cold would be sufficient to cool both the water for the apparatus for separating the mixture and the apparatus for separating air.
    • SUMMARY OF THE INVENTION
  • In certain embodiment, the invention proposes, according to certain alternatives, another use for the dry residual gases. They can as such be saturated with water in a tower that operates by direct contact, making it possible as such to lower the temperature of the unevaporated water and produce chilled water. The method is commonly used on the apparatuses for separating air in “water-nitrogen towers” in order to cool the water by heat exchange and evaporation with the cold nitrogen coming from the apparatus for separating air.
  • For the case where the incondensable items have a flow rate relative to the total flow treated that is clearly lower than nitrogen in relation to the air, a first portion of the cooling of the water could be carried out in a “non-condensable water” tower, with the first portion of the cooling being supplemented by a second portion of cooling in a refrigeration unit.
  • When an apparatus for separating air having a water cooling tower located in the vicinity of an apparatus for separating a mixture of carbon dioxide and at least one other gas, using the water-nitrogen tower in order to produce cold water for the two apparatuses and also possibly saturating therein the incondensable items (which will then share the venting of the nitrogen) will allow for genuine gains in investment in relation to using two independent towers.
  • The CO2 contained in the incondensable items must be prevented at all cost from rising back up to the apparatus for separating air via the line for transferring the dry nitrogen to the water-nitrogen tower. In normal operation as in the case of degraded mode, there is a real risk of introducing CO2 into the apparatus for separating air and of clogging it when the CO2 has frozen.
  • It can as such be considered to introduce the CO2 at a second level in the tower, above the nitrogen.
  • Note however that the risk is similar to that of allowing moisture to enter the cold box of the apparatus for separating air, except in that the incondensables arrive under pressure whereas when the nitrogen has become wet, it necessarily is at a pressure that is lower than at which it was in the box since it comes from there.
  • A precautionary measure, which is claimed as inventive also, consists in expanding the incondensable items sufficiently far from the tower so that over a distance that will be deemed as reasonable, the pressure in the supply pipe of the tower is lower for the line of incondensable items than for the line of nitrogen.
  • According to a particularly simple alternative, the process consists in cooling the water by using nitrogen from an ASU and possibly at least one gas coming from a unit for separating a mixture of CO2 and at least one other gas, which can for example be nitrogen, oxygen, argon, carbon monoxide, hydrogen, methane, NO2 or a mixture of at least two of these gases.
  • According to an object of the invention, an integrated apparatus is provided for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation comprising a unit for separating a gaseous mixture comprising carbon dioxide at and least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and a unit for separating air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that it comprises a water cooling tower that operates by direct contact as well as a line for sending water to the top of the tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the tower, a cooled water line for withdrawing cooled water from the tower and means for cooling the air upstream of the air separation unit, the cooled water line being connected to means for cooling the air upstream of the air separation unit and to the inlet and/or to the outlet of the unit for separating the gaseous mixture.
  • According to other optional aspects of the invention:
      • the means for cooling the air upstream of the air separation unit are constituted of a water cooling tower and a line for sending heated water from the scrubbing tower to the water cooling tower;
      • the cooled water line is adapted to send cooled water from the tower to the unit for separating the mixture in order to provide refrigeration to the gaseous mixture to be separated and/or to a product of the separation;
      • the integrated apparatus comprises an oxy-fuel combustion unit, a line for sending the oxygen from a (from the) apparatus for separating air to the oxy-fuel combustion unit and a line for sending fumes from the oxy-fuel combustion to the unit for separating a mixture as a gaseous mixture;
      • the apparatus comprises a line for sending the carbon dioxide depleted gas to the water cooling tower and wherein possibly the level of introduction of the nitrogen-enriched gas stream is lower than the level of the tower to which the carbon dioxide depleted gas is sent;
      • the apparatus comprises a mechanical refrigeration unit in order to cool the water cooled in the cooling tower upstream of the means for cooling the air upstream of the air separation unit and/or before it is sent to the unit for separating the gaseous mixture.
  • According to another object of the invention, an integrated process is provided for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation comprising a unit for separating a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and a unit for separating air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that water is cooled in a water cooling tower that operates by direct contact with the nitrogen-enriched gas stream, the air intended for the air separation unit is cooled with the cooled water in the cooling tower and the gaseous mixture intended for the unit for separating the gaseous mixture and/or a product from the unit for separating the gaseous mixture is cooled using the cooled water coming from the cooling tower.
  • According to other optional aspects:
      • the air is cooled upstream of the air separation unit in a scrubbing tower with water supplied by water cooled in the water cooling tower;
      • oxygen from one (from the) apparatus for separating air is sent to an oxy-fuel combustion unit and fumes from the oxy-fuel combustion are sent to the unit for separating a mixture as a gaseous mixture;
      • carbon dioxide depleted gas is sent from the unit for separating the gaseous mixture in the water cooling tower;
      • the level of introduction of the nitrogen-enriched gas stream is lower than the level of the tower where the carbon dioxide depleted gas is sent;
      • the water cooled in the cooling tower is cooled by means of a mechanical refrigeration unit, upstream of the means for cooling the air upstream of the air separation unit and upstream of the unit for separating the gaseous mixture;
      • the carbon dioxide depleted gas is expanded in a valve to a pressure that is lower than that at which the nitrogen-enriched gas stream is introduced in the water cooling tower;
      • at least one other gas in the mixture is nitrogen, oxygen, argon, hydrogen, carbon monoxide, methane or NO2 and the mixture contains at least 40 mol. % of carbon dioxide;
      • at least one other gas in the mixture is chosen from the list comprising hydrogen, carbon monoxide or methane and a wet gas exiting the top of the water cooling tower is used as a fuel, for example in a gas turbine;
      • the unit for separating the gaseous mixture separates the mixture by distillation and/or phase separation at sub-ambient temperature.
  • According to another object of the invention, an integrated apparatus is provided for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation comprising a unit for separating a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and an air separation unit by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that it comprises a water cooling tower that operates by direct contact as well as a line for sending water to the top of the tower, a line for sending carbon dioxide depleted gas to a lower level of the tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the tower, a cooled water line for withdrawing cooled water from the tower, means for cooling the air upstream of the air separation unit, the cooled water line being connected to the means for cooling the air upstream of the air separation unit.
  • According to other optional aspects:
      • the means for cooling the air upstream of the air separation unit are constituted of a scrubbing tower with water and a line for sending heated water from the scrubbing tower to the water cooling tower;
      • the apparatus comprises a line for sending cooled water from the tower to the unit for separating the mixture in order to provide refrigeration;
      • the apparatus comprises an apparatus such as described hereinabove comprising an oxy-fuel combustion unit, a line for sending oxygen from an apparatus for separating air to the oxy-fuel combustion unit and a line for sending fumes from the oxy-fuel combustion to the unit for separating a mixture as a gaseous mixture;
      • the nitrogen-enriched gas stream is sent to a level of the water cooling tower that is lower than that at which the carbon dioxide depleted gas is sent;
      • the line for sending at least one portion of the nitrogen-enriched gas stream from the air separation unit is connected to the lower level of the tower without passing through a turbine or an exchanger intended to cool the gaseous mixture.
  • According to another objet of the invention, an integrated process is provided for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation in an installation comprising a unit for separating a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and a unit for separating air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream characterised in that the installation comprises a water cooling tower that operates by direct contact as well as a line for sending water to the top of the tower, and wherein carbon dioxide depleted gas is sent to a lower level of the tower, at least one portion of the nitrogen-enriched gas stream is sent to a lower level of the tower, cooled water is withdrawn from the tower, the air is cooled in means in order to cool the air upstream of the air separation unit and cooled water is sent from the tank of the tower to the means for cooling the air upstream of the air separation unit.
  • According to other optional characteristics:
      • the air upstream of the air separation unit is cooled by direct exchange with cooled water coming from the water cooling tower;
      • the cooled water is sent from the water cooling tower to the unit for separating the mixture in order to provide refrigeration either upstream or downstream of the separation, with the water being taken either upstream or downstream of a mechanical refrigeration unit of the water cooled in the water cooling tower;
      • the carbon dioxide depleted gas is expanded in a valve to a pressure lower than that at which the nitrogen-enriched gas stream is introduced in the water cooling tower;
      • at least one other gas in the mixture is nitrogen, oxygen, argon, hydrogen, carbon monoxide, methane or NO2 and the mixture contains at least 40 mol. % of carbon dioxide;
      • at least one other gas comprises hydrogen, carbon monoxide or methane and a wet gas exiting the top of the water cooling tower is used as a fuel, for example in a gas turbine;
      • the nitrogen-enriched stream is sent from the apparatus for separating air to the tower without having been expanded and without having been heated in a cooling exchanger of the gaseous mixture;
      • the operating pressure of the tower is substantially equal to the pressure at which the nitrogen exits the apparatus for separating air.
  • An advantage of this invention is that it allows for the integration of production of cold water for apparatuses for separating with as the only connection between the two apparatuses a cooled water line, although a solution according to prior art requires a nitrogen line under pressure that connects the two apparatuses.
    • BRIEF DESCRIPTION OF THE DRAWINGS
  • These and other features, aspects, and advantages of the present invention will become better understood with regard to the following description, claims, and accompanying drawings. It is to be noted, however, that the drawings illustrate only several embodiments of the invention and are therefore not to be considered limiting of the invention's scope as it can admit to other equally effective embodiments.
  • FIG. 1 shows an embodiment of the invention.
  • FIG. 2 shows an embodiment of the invention.
  • FIG. 3 shows an embodiment of the invention.
  • FIG. 4 shows an embodiment of the invention.
    •  DETAILED DESCRIPTION
  • The invention shall be described in more detail by referring to the figures.
  • FIG. 1 shows an apparatus and an integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation according to the invention. FIGS. 2 to 4 show the details of various water cooling towers used to cool the air upstream of the air separation by distillation in FIG. 1, according to the invention. In FIG. 1, a stream of air 1 is cooled in a pre-cooling unit P comprising an air scrubbing tower with water and a water cooling tower with nitrogen 17. This type of cooling is well known in the “Industrial Gas Handbook” by F. G. Kerry, page 112. The air 3 cooled in the pre-cooling unit P is sent to an apparatus for separating air ASU wherein it is purified in order to remove the carbon dioxide and the moisture, cooled and separated in a system of columns in order to produce oxygen 5 and nitrogen 17. The oxygen 5 is sent to an oxy-fuel combustion boiler B also supplied with fuel 7. Fumes 9 coming from the oxy-fuel combustion unit B contain at least 40 mol. % of carbon dioxide on a dry basis, or even at least 60 mol. % of carbon dioxide, and at least one component chosen from the following list: nitrogen, oxygen, argon, hydrogen, carbon monoxide, methane or NO2. The fumes are treated in a separating unit CPU. Upstream of the CPU, the fumes 9 are cooled in a cooling unit R by heat exchange with cold water 15. The fumes are possibly compressed and then separated by phase separation and/or distillation in the unit CPU at a sub-ambient temperature. This makes it possible to produce a carbon dioxide-enriched stream CO2 in liquid or gaseous form 20 and a carbon dioxide depleted gas stream 13. The carbon dioxide depleted stream 13 can be a stream of nitrogen, oxygen, argon or NO2 or a mixture of at least two of these gases. The stream 13 exits the unit CPU at a temperature close to ambient temperature (−10° C. to 80° C.) and a pressure close to atmospheric pressure (1 bar a to 2 bars a) and is expanded in a valve V at a pressure of a few tens to a few hundred millimetres of water column according to load losses of the system downstream. The expanded gas 13 can be sent to pre-cooling.
  • The nitrogen 17 is sent directly from the apparatus for separating air ASU to the pre-cooling unit P without passing through another means of treatment, such as a turbine or an exchanger other than the air cooling exchanger associated with the apparatus for separating air ASU.
  • The pre-cooling unit produces cold water which is sent either to the unit R as a stream 15 or is used in the unit P or both.
  • FIG. 2 shows detail of the pre-cooling unit P.
  • This unit comprises a cooling tower 33 wherein the water 31 comes into direct contact with nitrogen 17 coming from the apparatus for separating air ASU. The expanded gas 13 can be sent to the tower at a level higher than the inlet level of the nitrogen 17, possibly separated from the inlet level of the nitrogen by a lining stage. The nitrogen 17 comes from the apparatus ASU directly and arrives in the tower 33 without passing through the elements R or CPU.
  • The water cooling tower 33 is supplied at the top by a stream of water 31 at a temperature from 4° C. to 40° C. The pressure of the stream 13 is slightly less than that of the stream 17 at the inlet in the tower 33, thanks to the expansion in the valve V upstream of the tower, in order to prevent polluting the cooled water.
  • The gas 17 and possibly the gas 13 cool the water by direct contact and evaporation of a portion of the water in these dry gases and the mixture formed 39 exits at the top of the tower as venting. The water heated in the unit CPU can be sent back to the unit P via the supply 21.
  • The cooled water in the tank of the tower 33 is pumped by a pump 25 in order to be sent to the air cooling tower with water by the line 27. Otherwise the cooled water can be sent to an exchanger with indirect contact in order to transfer refrigeration to the air intended for the distillation. A portion of this water 27 can also be used to provide refrigeration to the unit CPU, for example upstream of the desiccation unit.
  • This process may possibly not use a mechanical refrigeration unit such as a refrigeration unit. The tower 33 will possibly be somewhat larger than that used solely for providing water for the air separation unit ASU.
  • For the processes of FIGS. 3 and 4, a refrigeration unit 35 is used. In this way, instead of having a refrigeration unit for each of the units, a single refrigeration unit can cool the air separation unit ASU and the unit for separating the mixture containing carbon dioxide CPU.
  • FIG. 3 shows detail of the pre-cooling unit P.
  • This unit P comprises a cooling tower 33 wherein the water 31 comes into contact direct with nitrogen 17 coming from the apparatus for separating air ASU and an air cooling tower with water 133. The expanded gas 13 is possibly sent to the tower 33 at a level higher than the inlet level of the nitrogen 17. The nitrogen 17 comes from the apparatus ASU directly and arrives in the tower 33 without passing through the elements R or CPU.
  • The water cooling tower 33 is supplied at the top by a stream of water 31 at a temperature from 10° C. to 50° C.
  • The pressure of the stream 13 is slightly less than that of the stream 17 at the inlet in the tower 33, thanks to the expansion in the valve V upstream of the tower. The operating pressure of the tower 33 is substantially equal to the pressure at which the nitrogen 17 exits the apparatus for separating air ASU.
  • The gas 17 and possibly the gas 13 cool the water by direct contact and evaporation and the mixture formed 39 exits at the top of the tower as venting.
  • The cooled water in the tank of the tower 33 is pumped by a pump 25 in order to be sent to the top of the air cooling tower with water 133 as a stream 37. The air 1 intended for the distillation is cooled by being sent to the tank of the tower 133. The cooling water 21 is sent to an intermediate level of the tower 133 as a stream 121 and to the top of the tower 33 as a stream 31. The water cools the air by producing, at the top of the tower 133, a stream of cooled air 3 which is sent for purification and then for distillation in the air separation unit ASU.
  • The heated water 221 is collected in the tank of the tower 133 and is recycled in the tower 133 after exterior refrigeration (by using air coolers, through exchange with cold water, etc.). It can also be considered that the water 221 is not recycled but returns, for example, to a river or a water network downstream.
  • The cooled water 23 collected in the tank of the tower 33 is pressurised by the pump 25 and a portion 15 is sent to the separation unit CPU. The rest of the water is cooled by a refrigeration unit 35 in order to constitute the stream 37 sent to the top of the tower 133.
  • FIG. 4 differs from FIG. 3 only in that all of the water coming from the pump 25 is cooled in the refrigeration unit before it is divided into two. The cooled stream 37 is sent to the top of the tower 133 and the cooled stream 15 is sent to the unit CPU.
  • The cooled water 15 sent to the CPU can be used to cool the mixture to be separated or to cool a product from the separation. The unit CPU does not necessarily operate at sub-ambient temperature. The water heated in the unit CPU can be sent to the unit P via the supply 21.
  • The apparatus for separating air ASU does not necessarily supply an oxy-fuel combustion unit, if present, with oxygen. It is sufficient for the apparatus for separating air ASU to be located relatively close to the unit CPU to allow for the integration between the two.
  • For the case wherein the carbon dioxide depleted gas comprises carbon monoxide and/or methane and/or hydrogen, the gas can be sent to the cooling tower and the wet gas formed at the top of the tower can be used as a fuel, for example in a gas turbine.
  • While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.
  • The singular forms “a”, “an” and “the” include plural referents, unless the context clearly dictates otherwise.
  • “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.
  • “Providing” in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
  • Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.
  • Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.
  • All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.

Claims (18)

1-15. (canceled)
16. An apparatus for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation, the apparatus comprising:
a CO2 separation unit configured to separate a gaseous mixture comprising carbon dioxide and at least one other gas in order to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas;
an air separation unit (ASU) configured to separate air by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream; and
a water cooling tower that operates by direct contact as well as a line for sending water to the top of the water cooling tower, a line for sending at least one portion of the nitrogen-enriched gas stream to a lower level of the water cooling tower, a cooled water line for withdrawing cooled water from the water cooling tower and means for cooling the air upstream of the air separation unit, the cooled water line being connected to means for cooling the air upstream of the air separation unit and to the inlet and/or to the outlet of the CO2 separation unit.
17. The apparatus as claimed in claim 16, wherein the means for cooling the air upstream of the ASU comprises a scrubbing tower with water.
18. The apparatus as claimed in claim 17, wherein the means for cooling the air upstream of the ASU further comprises a line configured to send heated water from the scrubbing tower to the water cooling tower.
19. The apparatus as claimed in claim 16, wherein the cooled water line is configured to send cooled water from the tower to the CO2 separation unit such that refrigeration is provided to the gaseous mixture to be separated or to a product from the separation.
20. The apparatus as claimed in claim 16, further comprising an oxy-fuel combustion unit, a line for sending oxygen from the ASU to the oxy-fuel combustion unit and a line for sending fumes from the oxy-fuel combustion to the CO2 separation unit .
21. The apparatus as claimed in claim 16, further comprising a line configured to send the carbon dioxide depleted gas to the water cooling tower and wherein possibly the level of introduction of the nitrogen-enriched gas stream is lower than the level of the tower where the carbon dioxide depleted gas is sent.
22. The apparatus as claimed in claim 16, further comprising a mechanical refrigeration unit configured to cool the water cooled in the cooling tower upstream of the means for cooling the air upstream of the ASU and/or before it is sent to the CO2 separation unit.
23. The apparatus as claimed in claim 16, wherein the line for sending at least one portion of the nitrogen-enriched gas stream from the ASU is connected to a lower level of the tower without passing through a turbine or an exchanger configured to cool the gaseous mixture.
24. An integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by air distillation, comprising a CO2 separation unit configured to separate a gaseous mixture comprising carbon dioxide and at least one other gas to produce a carbon dioxide-enriched gas and a carbon dioxide depleted gas and an air separation unit by cryogenic distillation in order to produce at least one nitrogen-enriched gas stream wherein the water is cooled in a water cooling tower that operates by direct contact with the nitrogen-enriched gas stream, the air intended for the air separation unit is cooled with water cooled in the cooling tower and the gaseous mixture intended for the CO2 separation unit and/or a product from the CO2 separation unit is cooled using the cooled water coming from the cooling tower.
25. The process as claimed in claim 24, wherein the air upstream of the air separation unit is cooled in a scrubbing tower with water supplied by water cooled in the water tooling tower.
26. The process as claimed in claim 24, further comprising the steps of sending the oxygen from the ASU to an oxy-fuel combustion unit; and sending fumes from the oxy-fuel combustion to the CO2 separation unit.
27. The process as claimed in claim 24, further comprising sending carbon dioxide depleted gas from the CO2 separation unit to the water cooling tower,
28. The process as claimed in claim 27, wherein the level of introduction of the nitrogen-enriched gas stream is lower than the level of the tower where the carbon dioxide depleted gas is sent.
29. The process as claimed in claim 24, wherein the cooled water is cooled in the cooling tower by means of a mechanical refrigeration unit before sending it to the means for cooling air upstream of the air separation unit and/or before sending it to the CO2 separation unit.
30. The process as claimed in claim 24, wherein the carbon dioxide depleted gas is expanded in a valve to a pressure lower than that at which the nitrogen-enriched gas stream is introduced in the water cooling tower.
31. The process as claimed in claim 24, wherein at least one other gas in the mixture is selected from the group consisting of nitrogen, oxygen, argon, hydrogen, carbon monoxide, methane, NO2, and combinations thereof, and the mixture contains at least 40 mol. % of carbon dioxide.
32. The process as claimed in claim 24, wherein at least one other gas in the mixture is selected from the group consisting of hydrogen, carbon monoxide, methane, and combinations thereof, and wherein a wet gas exiting from the top of the water cooling tower is used as a fuel.
US14/122,255 2011-05-31 2012-05-29 Apparatus and Integrated Process for Separating a Mixture of Carbon Dioxide and at Least One Other Gas and for Separating Air by Cryogenic Distillation Abandoned US20140208798A1 (en)

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FR1154754A FR2976059B1 (en) 2011-05-31 2011-05-31 INTEGRATED APPARATUS AND METHOD FOR SEPARATING A MIXTURE OF CARBON DIOXIDE AND AT LEAST ONE OTHER GAS AND AIR SEPARATION BY CRYOGENIC DISTILLATION
FR1154754 2011-05-31
PCT/FR2012/051203 WO2012164220A2 (en) 2011-05-31 2012-05-29 Apparatus and integrated process for separating a mixture of carbon dioxide and at least one other gas and for separating air by cryogenic distillation

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EP2715260A2 (en) 2014-04-09
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