US20060156922A1 - Method and apparatus for treating a gas by adsorption in particular for purifying atomspheric air - Google Patents
Method and apparatus for treating a gas by adsorption in particular for purifying atomspheric air Download PDFInfo
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- US20060156922A1 US20060156922A1 US11/327,878 US32787806A US2006156922A1 US 20060156922 A1 US20060156922 A1 US 20060156922A1 US 32787806 A US32787806 A US 32787806A US 2006156922 A1 US2006156922 A1 US 2006156922A1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
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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
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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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- 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
- F25J3/04—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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04775—Air purification and pre-cooling
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
- B01D2259/4005—Nature of purge gas
- B01D2259/40052—Recycled product or process gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
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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
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
- F25J2205/70—Heating the adsorption vessel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/06—Adiabatic compressor, i.e. without interstage cooling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- 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 provides a process and apparatus for treating a gas by adsorption wherein additional heat is provided to the regeneration fluid by external means prior to its use in the regeneration process.
- the device and process of the present invention comprise the steps of:
- the invention applies in particular to the separation of atmospheric air by distillation, said separation comprising an air compression step with a view to a subsequent step of cooling this air, and a step of stripping water and carbon dioxide from said air by flowing through an adsorber for the purpose of preventing the formation of ice and/or dry ice in the heat exchanger that brings the air to the cryogenic distillation temperatures.
- the adsorber When the gas treatment process in question is not carried out on an occasional basis but is intended, on the contrary, to be repeated or even operated continuously, the adsorber must be periodically regenerated.
- FIG. 1 illustrates an apparatus similar to that described in EP 0 456 575, FIG. 3;
- FIG. 2 illustrates a novel variant of the apparatus of the present invention
- FIG. 3 illustrates a cryogenic air separation installation incorporating the apparatus of FIG. 1 ;
- FIGS. 4 to 6 illustrate three alternative embodiments of the apparatus according to the present invention.
- cryogenic distillation produces a waste gas that is dry and decarbonated, and consequently capable of regenerating the adsorber.
- the available mean flow rate of regeneration fluid may be limited. It may also be desirable to intentionally limit the consumption of regeneration fluid.
- EP 0 456 575 proposes (FIG. 3) a process of the aforementioned type in which there is heat exchange between the compressed gas and the regeneration fluid for the adsorber.
- the subject of the invention is a treatment process of the aforementioned type, characterized in that the process furthermore includes a step consisting in additionally heating the regeneration fluid coming from step (c1) by means of an auxiliary heat injection, before this regeneration fluid is made to pass through the adsorber.
- the subject of the invention is also an apparatus for treating a gas by adsorption, of the type comprising:
- the apparatus 1 illustrated in FIG. 1 comprises a compressor 2 , a heat exchanger 3 and an adsorption unit 4 .
- a first line 5 forms a circuit for flow of the gas to be treated, which links the compressor 2 with the exchanger 3 and the adsorption unit 4 .
- Said line is arranged in such a way that the gas to be treated, drawn in by the compressor 2 , is discharged by the latter, then passes through the exchanger 3 and then the adsorption unit 4 .
- a second line 6 intended to transport a regeneration fluid links the exchanger 3 with the adsorption unit 4 . It is arranged in such a way that the regeneration fluid passes firstly through the exchanger 3 and then the adsorption unit 4 .
- the adsorption unit 4 comprises identical first and second adsorbers 7 and 8 and a switching device (not shown) which, in a first position, links, on the one hand, the first adsorber 7 , then operating in adsorption mode, to the first line 5 and, on the other hand, the second adsorber 8 to the second line 6 , this second adsorber 8 then being regenerated by the regeneration fluid passing through it.
- a switching device which, in a first position, links, on the one hand, the first adsorber 7 , then operating in adsorption mode, to the first line 5 and, on the other hand, the second adsorber 8 to the second line 6 , this second adsorber 8 then being regenerated by the regeneration fluid passing through it.
- these two adsorbers 7 and 8 are switched over, the first 7 being in regeneration mode while the second 8 is in an active adsorption state.
- the adsorption unit 4 may have more than two adsorbers. It may also have only one adsorber, the apparatus 1 for treating a gas by adsorption then being provided with at least one buffer volume in order to allow it to operate continuously.
- the adsorption unit 4 is illustrated when the switching device is in its first position.
- the exchanger 3 is of the countercurrent type, as may be seen in FIG. 1 .
- this exchanger 3 intended to bring two gases into indirect heat exchange relationship, will usefully be of the brazed-plate type.
- the regeneration fluid flows in the second line 6 so that it passes firstly through the exchanger 3 and then the adsorption unit 4 .
- the apparatus 1 for treating a gas by adsorption that has just been described is intended to operate continuously.
- the gas to be treated enters the apparatus 1 via the inlet 9 for the gas to be treated, which corresponds to the intake of the compressor 2 . It is then compressed by this compressor 2 , consequently experiencing a temperature rise. Its temperature is then above that of the regeneration fluid that enters the treatment device 1 via the regeneration fluid inlet 10 .
- the gas to be treated and the regeneration fluid then each flow separately through the exchanger 3 , during which flow they are brought into countercurrent indirect heat exchange relationship so as to heat the regeneration fluid and at the same time cool the gas to be treated.
- the gas to be treated and the regeneration fluid each flow separately into the adsorption unit 4 via two different inlets.
- the gas to be treated and the regeneration fluid pass through one of the respective two adsorbers 7 and 8 , depending on the position of the switching device.
- the adsorber through which the gas to be treated flows is active and operates in adsorption mode so as to adsorb at least one particular component present in the gas to be treated.
- the adsorber through which the regeneration fluid flows is itself regenerated, countercurrently with respect to the direction of flow of the gas to be treated in adsorption phase.
- the two adsorbers 7 and 8 are switched over by the switching device, so that the adsorber that was in adsorption mode is regenerated, whereas the one which was in regeneration mode becomes active and adsorbs at least one particular constituent of the gas to be treated that is flowing through it.
- the treated gas after having passed through one of the two adsorbers, exits the treatment apparatus 1 , via an outlet 11 for the treated gas, where it is available in the compressed and adsorptively purified state.
- this is exhausted from the treatment apparatus 1 at 12 .
- the gas treatment apparatus 1 ′ illustrated in FIG. 2 comprises substantially the same components as the one, shown in FIG. 1 , which has just been commented upon.
- the apparatus furthermore includes additional heating means 13 for heating the regeneration fluid.
- a first solution may consist in increasing the flow rate of the regeneration fluid.
- the regenerability of the regeneration fluid may be increased by using said additional heating means 13 .
- the triple-flow exchanger 3 ′ replaces the exchanger 3 .
- the additional heating means 13 comprise an auxiliary heat source 14 , for example an electrical heat source, linked by a circuit 15 to the hot part of the heat exchanger 3 ′.
- the circuit 15 forms a closed loop for the flow of a heat-transfer fluid between said auxiliary heat source 14 and the exchanger 3 ′.
- Means move the heat-transfer fluid inside the circuit 15 .
- the flow of the heat-transfer fluid through the exchanger 3 ′ is in the opposite direction to the flow of the regeneration fluid, in order to operate as a countercurrent exchanger.
- the configuration of the triple-flow exchanger 3 ′ illustrated in FIG. 2 is such that the regeneration fluid is firstly heated by countercurrent heat exchange with just the gas to be treated, in the cold part 103 ′ of the exchanger, and then secondly heated by countercurrent heat exchange with just the heat-transfer fluid in the hot part 203 ′ of the exchanger.
- This alternative embodiment reproduces the operation of the treatment apparatus 1 of FIG. 1 , but includes an additional step in which the regeneration fluid, after having been heated by heat exchange with the gas to be treated, undergoes further heat exchange with the additional heating means 13 in order to raise its temperature even further and thus increase its regenerability.
- the heating means 14 transmit a certain quantity of heat to the heat-transfer fluid which, in turn, restores this quantity of heat to the regeneration fluid within the triple-flow exchanger 3 ′.
- the heating means 14 may be placed directly in the second line 6 that transports the regeneration fluid, the triple-flow exchanger 3 ′ then reverting to a simple exchanger 3 of the type shown in FIG. 1 .
- additional cooling means may be provided for cooling the gas to be treated, which means may advantageously be placed between the heat exchanger 3 or 3 ′ and the adsorption unit 4 , as indicated by the dot/dash lines at 3 A and 3 ′A in FIGS. 1 and 2 .
- the additional step thus obtained, of cooling the gas to be treated, then promotes the adsorption effect.
- FIG. 3 shows schematically a cryogenic air separation installation for producing particularly oxygen. It incorporates, placed upstream, the treatment apparatus 1 of FIG. 1 , which apparatus is connected to what is commonly referred to as the cold box 16 .
- Said cold box 16 comprises a countercurrent heat exchange line 17 and a double distillation column 18 .
- the double column 18 has an inlet 19 , for feeding its medium-pressure column with air, an oxygen gas production outlet 20 and an outlet 21 for the waste gas (impure nitrogen), said outlet being provided on its low-pressure column.
- the inlet 19 and the outlets 20 and 21 are respectively linked by means of lines 22 , 23 and 23 A to the air outlet 24 , to the oxygen inlet 25 and to the waste gas inlet 26 at the cold end of the exchanger 17 .
- the other parts of the cold box 16 known per se, have not been shown.
- the inlet 9 of the treatment apparatus 1 is linked to an atmospheric air intake.
- the outlet 11 of this same apparatus 1 which delivers compressed, dry and decarbonated air, is linked to that one of the inlets of the exchanger 17 , at the hot end of the latter, which communicates with the outlet 24 .
- the waste gas which leaves the double column 18 via 23 , is, as is known, at a slight overpressure, which allows it to pass through a certain number of components in which its pressure decreases until the gas is finally discharged into the atmosphere.
- the waste gas 19 On leaving the exchanger 17 , the waste gas 19 has the qualities of a regenerating gas insofar as it is dry, decarbonated and depressurized.
- the outlet of the exchanger 17 via which the waste gas escapes is linked to the inlet 10 for the regeneration gas of the treatment apparatus 1 , the waste gas being used as regeneration fluid.
- the waste gas is at a temperature below that of the air leaving the compressor 2 .
- it will be heated, this having the effect of increasing its regenerability.
- the flow of the fluids within the cryogenic air separation installation that has just been commented upon is caused by the driving pressure produced by the compressor 2 .
- the exchanger 3 or 3 ′ may be a cross-current exchanger, which allows better optimization of the pipework and/or the head losses and/or the discharge of condensates.
- FIG. 4 shows a treatment apparatus according to the invention that differs from that of FIG. 2 in two aspects.
- the cold part 103 ′ is provided with an auxiliary refrigerating circuit 27 , which is itself refrigerated by an external cold source 28 .
- the refrigerating fluid flows countercurrently with the gas to be treated.
- the line 10 is provided, before its inlet at the cold end of the exchanger 3 ′, with a valve 29 and, upstream of said valve, a branch 30 that leads to the upper opening on one or other of the adsorbers 7 and 8 and is equipped with a valve 31 .
- the valve 31 When the adsorber in regeneration mode (in this case, the adsorber 8 ) has to be coursed by hot regeneration fluid, the valve 31 is closed, the valve 29 is open, the refrigerating circuit 27 is not in service and the heating circuit 13 is in service. The operation is then identical to that described above with regard to FIG. 2 .
- valves 29 and 31 are reversed so that the regeneration fluid passes directly into the adsorber via the line 30 .
- the heating circuit is closed off and the refrigerating circuit 27 is brought into service.
- the latter circuit refrigerates the compressed air flowing through the exchanger 3 ′.
- the embodiment shown in FIG. 5 differs from the previous one by the refrigerating circuit 27 being omitted and by the cold source 28 being installed on a branch-off 32 of the line 5 , starting upstream of the exchanger 3 ′ and reemerging downstream thereof.
- This branch-off is equipped with a valve 33 , and another valve 34 is added to the line 5 between the cold end of the exchanger 3 ′ and the outlet of the branch-off 32 .
- a line 35 is tapped off the line 6 .
- Two valves 36 and 37 provided in the lines 35 and 6 respectively, are used to direct the regeneration fluid coming from the exchanger 3 ′ either to the adsorber in regeneration mode or to the discharge point.
- valve 34 when it is the cold regeneration fluid that flows through the adsorber 8 ′ in regeneration mode, the valve 34 is closed, whereas the valve 33 is open, in such a way that the air is cooled by the cold source 28 .
- a small flow of gas to be treated and of regeneration fluid is maintained through the exchanger 3 ′, the latter being discharged via the line 35 , by operating the valves 36 and 37 .
- the embodiment shown in FIG. 6 differs from the previous one firstly by the omission of the components 28 , 32 , 33 and 34 and secondly by the addition of a line 38 that links the line 12 to the cold end of the refrigerating fluid passage of the exchanger 3 ′.
- This line 38 is equipped with a valve 39 , and another valve 40 is provided in the line 12 downstream of the line 35 .
- valve 40 when it is the cold regeneration fluid that flows through the adsorber 8 in regeneration mode, the valve 40 is closed and the valve 39 opened, in such a way that the regeneration fluid leaving the adsorber flows through the exchanger 3 ′. As previously, this flow serves to cool the compressed gas to be treated, which is then discharged via the line 35 .
- the apparatus furthermore includes additional heating means 13 for heating the regeneration fluid.
- a first solution may consist in increasing the flow rate of the regeneration fluid.
- the regenerability of the regeneration fluid may be increased by using said additional heating means 13 .
- the triple-flow exchanger 3 ′ replaces the exchanger 3 in FIG. 1 .
- the additional heating means 13 comprise an auxiliary heat source 14 , for example an electrical heat source, linked by a circuit 15 to the hot part of the heat exchanger 3 ′.
- the circuit 15 forms a closed loop for the flow of a heat-transfer fluid between said auxiliary heat source 14 and the exchanger 3 ′.
- Means move the heat-transfer fluid inside the circuit 15 .
- the flow of the heat-transfer fluid through the exchanger 3 ′ is in the opposite direction to the flow of the regeneration fluid, in order to operate as a countercurrent exchanger.
- the configuration of the triple-flow exchanger 3 ′ illustrated in FIGS. 4 to 6 is such that the regeneration fluid is firstly heated by countercurrent heat exchange with just the gas to be treated, in the cold part 103 ′ of the exchanger, and then secondly heated by countercurrent heat exchange with just the heat-transfer fluid in the hot part 203 ′ of the exchanger.
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Abstract
Method and apparatus for treating a gas by adsorption. A gas is compressed and then treated by being circulated in an adsorber. A regenerating fluid is indirectly heated by the gas coming from the compressor. In a second regeneration phase, the regenerating fluid is sent directly to the adsorber, while the treated gas is refrigerated by an auxiliary refrigerator
Description
- This application is a Continuation-In-Part of U.S. patent application Ser. No. 10/492,491, filed Apr. 9, 2004, the entire contents of which are incorporated herein by reference.
- The present invention provides a process and apparatus for treating a gas by adsorption wherein additional heat is provided to the regeneration fluid by external means prior to its use in the regeneration process. The device and process of the present invention comprise the steps of:
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- (a) compressing the gas to be treated;
- (b) making the gas to be treated from step (a) flow through an adsorber in adsorption phase;
- (c) making a stream of regeneration fluid flow through the adsorber in the regeneration phase, and
- (c1) during a first part of the adsorber regeneration phase, indirect heat exchange between the gas to be treated from step (a) and the refrigeration fluid stream is established in a heat exchanger so as to cool the gas to be treated from step (a) and intended for step (b) and to heat the regeneration fluid intended for step (c);
- (c2) during a second part of the adsorber regeneration phase, the regeneration fluid is made to flow through the adsorber without making it undergo the heat exchange of step (c1); and
- (d) auxiliary refrigeration of the gas to be treated during said step (c2) is carried out.
- The invention applies in particular to the separation of atmospheric air by distillation, said separation comprising an air compression step with a view to a subsequent step of cooling this air, and a step of stripping water and carbon dioxide from said air by flowing through an adsorber for the purpose of preventing the formation of ice and/or dry ice in the heat exchanger that brings the air to the cryogenic distillation temperatures.
- When the gas treatment process in question is not carried out on an occasional basis but is intended, on the contrary, to be repeated or even operated continuously, the adsorber must be periodically regenerated.
- For a further understanding of the nature and objects for the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers and wherein:
-
FIG. 1 illustrates an apparatus similar to that described inEP 0 456 575, FIG. 3; -
FIG. 2 illustrates a novel variant of the apparatus of the present invention; -
FIG. 3 illustrates a cryogenic air separation installation incorporating the apparatus ofFIG. 1 ; and - FIGS. 4 to 6 illustrate three alternative embodiments of the apparatus according to the present invention.
- For this purpose, it is known to use a regeneration gas that is made to flow through the adsorber. At least two adsorbers are then used, which switch alternately between an adsorption phase and a regeneration phase.
- In the intended application, the cryogenic distillation produces a waste gas that is dry and decarbonated, and consequently capable of regenerating the adsorber.
- The available mean flow rate of regeneration fluid may be limited. It may also be desirable to intentionally limit the consumption of regeneration fluid.
- It is also known to improve the regenerability of the regeneration fluid by heating it, for example by electrical heating means or by steam, before making it flow through the adsorber.
- However, this solution is expensive as it consumes energy.
- To reduce the amount of energy consumed and/or the amount of regeneration fluid consumed, for the same result in terms of quantity and treatment quality of the heated gas,
EP 0 456 575 proposes (FIG. 3) a process of the aforementioned type in which there is heat exchange between the compressed gas and the regeneration fluid for the adsorber. - It is an object of the invention to improve this known process in order to allow it to carry out regeneration in two successive steps, one with heated regeneration fluid, without adding a further exchanger, the other with unheated regeneration fluid.
- For this purpose, the subject of the invention is a treatment process of the aforementioned type, characterized in that the process furthermore includes a step consisting in additionally heating the regeneration fluid coming from step (c1) by means of an auxiliary heat injection, before this regeneration fluid is made to pass through the adsorber.
- According to other features of this process:
-
- said auxiliary refrigeration step (d) consists in refrigerating the gas to be treated by an auxiliary cold source;
- said auxiliary refrigeration step (d) consists in refrigerating the gas to be treated by at least one part of the stream of regeneration fluid that has passed through the adsorber;
- said auxiliary refrigeration is carried out in the heat exchanger;
- said refrigeration is carried out outside the heat exchanger;
- a flow of gas to be treated and of regeneration fluid is maintained in the heat exchanger during said auxiliary refrigeration step (d);
- the process furthermore includes a step consisting in additionally cooling the gas to be treated coming from step (c1), before this gas to be treated is made to pass through the adsorber; and
- the gas to be treated is atmospheric air, the function of step (b) is to strip water and carbon dioxide from the air to be treated coming from step (a), said process includes an additional step consisting in separating the air coming from step (b) by distillation in order to produce at least one of its constituents and also a waste gas, and the waste gas forms said regeneration fluid.
- The subject of the invention is also an apparatus for treating a gas by adsorption, of the type comprising:
-
- a compressor for compressing the gas to be treated, the delivery side of which compressor is designed to be connected to the inlet of at least one adsorber during an adsorption phase of the latter;
- means for making a regeneration fluid flow through the adsorber during a regeneration phase of the latter; and
- means for heating the regeneration fluid entering the adsorber in regeneration mode;
the heating means comprising a heat exchanger designed to bring the regeneration fluid into indirect heat exchange relationship with the gas coming from the compressor, the apparatus furthermore including branch-off means for sending the regeneration fluid into the adsorber in regeneration mode without passing through the heat exchanger, and auxiliary refrigerating means for refrigerating the gas to be treated when said branch-off means are activated, characterized in that the heating means furthermore comprise anauxiliary heat source 14 designed to carry out additional heating on the regeneration fluid.
- The
apparatus 1 illustrated inFIG. 1 comprises acompressor 2, aheat exchanger 3 and anadsorption unit 4. Afirst line 5 forms a circuit for flow of the gas to be treated, which links thecompressor 2 with theexchanger 3 and theadsorption unit 4. Said line is arranged in such a way that the gas to be treated, drawn in by thecompressor 2, is discharged by the latter, then passes through theexchanger 3 and then theadsorption unit 4. - A
second line 6 intended to transport a regeneration fluid links theexchanger 3 with theadsorption unit 4. It is arranged in such a way that the regeneration fluid passes firstly through theexchanger 3 and then theadsorption unit 4. - The
adsorption unit 4 comprises identical first andsecond adsorbers first adsorber 7, then operating in adsorption mode, to thefirst line 5 and, on the other hand, the second adsorber 8 to thesecond line 6, this second adsorber 8 then being regenerated by the regeneration fluid passing through it. In a second position of the switching device, these twoadsorbers - Of course, the
adsorption unit 4 may have more than two adsorbers. It may also have only one adsorber, theapparatus 1 for treating a gas by adsorption then being provided with at least one buffer volume in order to allow it to operate continuously. - In
FIG. 1 , theadsorption unit 4 is illustrated when the switching device is in its first position. - Advantageously, the
exchanger 3 is of the countercurrent type, as may be seen inFIG. 1 . - Moreover, this
exchanger 3, intended to bring two gases into indirect heat exchange relationship, will usefully be of the brazed-plate type. - The regeneration fluid flows in the
second line 6 so that it passes firstly through theexchanger 3 and then theadsorption unit 4. - The
apparatus 1 for treating a gas by adsorption that has just been described is intended to operate continuously. - The gas to be treated enters the
apparatus 1 via theinlet 9 for the gas to be treated, which corresponds to the intake of thecompressor 2. It is then compressed by thiscompressor 2, consequently experiencing a temperature rise. Its temperature is then above that of the regeneration fluid that enters thetreatment device 1 via theregeneration fluid inlet 10. - The gas to be treated and the regeneration fluid then each flow separately through the
exchanger 3, during which flow they are brought into countercurrent indirect heat exchange relationship so as to heat the regeneration fluid and at the same time cool the gas to be treated. - On leaving the
exchanger 3, the gas to be treated and the regeneration fluid each flow separately into theadsorption unit 4 via two different inlets. Inside theadsorption unit 4, the gas to be treated and the regeneration fluid pass through one of the respective twoadsorbers - In a subsequent step, the two
adsorbers - As is known, the use of at least two adsorbers therefore allows continuous operation.
- The treated gas, after having passed through one of the two adsorbers, exits the
treatment apparatus 1, via anoutlet 11 for the treated gas, where it is available in the compressed and adsorptively purified state. - As regards the regenerating gas, this is exhausted from the
treatment apparatus 1 at 12. - The
gas treatment apparatus 1′ illustrated inFIG. 2 comprises substantially the same components as the one, shown inFIG. 1 , which has just been commented upon. - The
exchanger 3 alone has been replaced with a triple-flow exchanger 3′ that will be commented upon below. The same references are retained for the components common to these two alterative embodiments of the invention, these common components being arranged one with respect to another in the same manner in both cases. - The apparatus furthermore includes additional heating means 13 for heating the regeneration fluid.
- This is because it may prove the case that the regeneration fluid is heated by heat exchange with the gas to be treated insufficiently for complete regeneration of an adsorber over the course of the entire adsorption/regeneration cycle. A first solution may consist in increasing the flow rate of the regeneration fluid. Alternatively or additionally to this first solution, the regenerability of the regeneration fluid may be increased by using said additional heating means 13.
- The triple-
flow exchanger 3′ replaces theexchanger 3. - The additional heating means 13 comprise an
auxiliary heat source 14, for example an electrical heat source, linked by acircuit 15 to the hot part of theheat exchanger 3′. Thecircuit 15 forms a closed loop for the flow of a heat-transfer fluid between saidauxiliary heat source 14 and theexchanger 3′. - Means (not shown) move the heat-transfer fluid inside the
circuit 15. Advantageously, as shown, the flow of the heat-transfer fluid through theexchanger 3′ is in the opposite direction to the flow of the regeneration fluid, in order to operate as a countercurrent exchanger. - The configuration of the triple-
flow exchanger 3′ illustrated inFIG. 2 is such that the regeneration fluid is firstly heated by countercurrent heat exchange with just the gas to be treated, in thecold part 103′ of the exchanger, and then secondly heated by countercurrent heat exchange with just the heat-transfer fluid in thehot part 203′ of the exchanger. - This alternative embodiment reproduces the operation of the
treatment apparatus 1 ofFIG. 1 , but includes an additional step in which the regeneration fluid, after having been heated by heat exchange with the gas to be treated, undergoes further heat exchange with the additional heating means 13 in order to raise its temperature even further and thus increase its regenerability. For this purpose, the heating means 14 transmit a certain quantity of heat to the heat-transfer fluid which, in turn, restores this quantity of heat to the regeneration fluid within the triple-flow exchanger 3′. - As a variant, the heating means 14 may be placed directly in the
second line 6 that transports the regeneration fluid, the triple-flow exchanger 3′ then reverting to asimple exchanger 3 of the type shown inFIG. 1 . - In addition, in one or the other of the two embodiments that have just been commented upon, additional cooling means may be provided for cooling the gas to be treated, which means may advantageously be placed between the
heat exchanger adsorption unit 4, as indicated by the dot/dash lines at 3A and 3′A inFIGS. 1 and 2 . The additional step thus obtained, of cooling the gas to be treated, then promotes the adsorption effect. -
FIG. 3 shows schematically a cryogenic air separation installation for producing particularly oxygen. It incorporates, placed upstream, thetreatment apparatus 1 ofFIG. 1 , which apparatus is connected to what is commonly referred to as thecold box 16. - Said
cold box 16 comprises a countercurrentheat exchange line 17 and adouble distillation column 18. Thedouble column 18 has aninlet 19, for feeding its medium-pressure column with air, an oxygengas production outlet 20 and anoutlet 21 for the waste gas (impure nitrogen), said outlet being provided on its low-pressure column. Theinlet 19 and theoutlets lines air outlet 24, to theoxygen inlet 25 and to thewaste gas inlet 26 at the cold end of theexchanger 17. The other parts of thecold box 16, known per se, have not been shown. - The
inlet 9 of thetreatment apparatus 1 is linked to an atmospheric air intake. Theoutlet 11 of thissame apparatus 1, which delivers compressed, dry and decarbonated air, is linked to that one of the inlets of theexchanger 17, at the hot end of the latter, which communicates with theoutlet 24. - The waste gas, which leaves the
double column 18 via 23, is, as is known, at a slight overpressure, which allows it to pass through a certain number of components in which its pressure decreases until the gas is finally discharged into the atmosphere. On leaving theexchanger 17, thewaste gas 19 has the qualities of a regenerating gas insofar as it is dry, decarbonated and depressurized. Thus, the outlet of theexchanger 17 via which the waste gas escapes is linked to theinlet 10 for the regeneration gas of thetreatment apparatus 1, the waste gas being used as regeneration fluid. It should be noted at this point that the waste gas is at a temperature below that of the air leaving thecompressor 2. Thus, as it passes through theexchanger 3, it will be heated, this having the effect of increasing its regenerability. - The operation of the
treatment apparatus 1 thereafter remains unchanged. - The flow of the fluids within the cryogenic air separation installation that has just been commented upon is caused by the driving pressure produced by the
compressor 2. - It will firstly be noted that, by placing the adsorber in the path of the gas to be treated after the compressor, the adsorption effect is promoted because this gas to be treated has been compressed. However, the temperature rise of this gas to be treated owing to this compression would have the effect of reducing the adsorption efficiency.
- By introducing a
heat exchanger 3 whose purpose is, on the one hand, to increase the temperature of the regeneration fluid and, on the other hand, to reduce the temperature of the gas to be treated, it is possible particularly inexpensively to increase the efficiency of the adsorption/regeneration cycle in two ways. This is because the increase in the temperature of the regeneration fluid promotes regeneration of the adsorber, and adsorption efficiency is improved owing to the cooling of the gas to be treated during its passage through theexchanger 3. - As a variant, the
exchanger -
FIG. 4 shows a treatment apparatus according to the invention that differs from that ofFIG. 2 in two aspects. - Firstly, the
cold part 103′ is provided with anauxiliary refrigerating circuit 27, which is itself refrigerated by an externalcold source 28. In this circuit, the refrigerating fluid flows countercurrently with the gas to be treated. - Secondly, the
line 10 is provided, before its inlet at the cold end of theexchanger 3′, with avalve 29 and, upstream of said valve, abranch 30 that leads to the upper opening on one or other of theadsorbers valve 31. - When the adsorber in regeneration mode (in this case, the adsorber 8) has to be coursed by hot regeneration fluid, the
valve 31 is closed, thevalve 29 is open, the refrigeratingcircuit 27 is not in service and theheating circuit 13 is in service. The operation is then identical to that described above with regard toFIG. 2 . - When, in a subsequent phase of the regeneration of the
adsorber 8, the latter must be coursed by cold regeneration fluid, thevalves line 30. - At the same time, the heating circuit is closed off and the refrigerating
circuit 27 is brought into service. Thus, it is the latter circuit that refrigerates the compressed air flowing through theexchanger 3′. - In this way, the thermal operation of the
exchanger 3′ varies little, thereby reducing thermal fatigue effects, especially if the exchanger is of the type with brazed aluminum plates. - The embodiment shown in
FIG. 5 differs from the previous one by the refrigeratingcircuit 27 being omitted and by thecold source 28 being installed on a branch-off 32 of theline 5, starting upstream of theexchanger 3′ and reemerging downstream thereof. This branch-off is equipped with avalve 33, and anothervalve 34 is added to theline 5 between the cold end of theexchanger 3′ and the outlet of the branch-off 32. In addition, aline 35 is tapped off theline 6. Twovalves lines exchanger 3′ either to the adsorber in regeneration mode or to the discharge point. - Thus, when it is the cold regeneration fluid that flows through the
adsorber 8′ in regeneration mode, thevalve 34 is closed, whereas thevalve 33 is open, in such a way that the air is cooled by thecold source 28. To achieve the same advantage of reducing thermal fatigue of the exchanger as in the case ofFIG. 4 , during regeneration of theadsorber 8 by cold regeneration fluid, a small flow of gas to be treated and of regeneration fluid is maintained through theexchanger 3′, the latter being discharged via theline 35, by operating thevalves - The embodiment shown in
FIG. 6 differs from the previous one firstly by the omission of thecomponents line 38 that links theline 12 to the cold end of the refrigerating fluid passage of theexchanger 3′. Thisline 38 is equipped with avalve 39, and anothervalve 40 is provided in theline 12 downstream of theline 35. - In this embodiment, when it is the cold regeneration fluid that flows through the
adsorber 8 in regeneration mode, thevalve 40 is closed and thevalve 39 opened, in such a way that the regeneration fluid leaving the adsorber flows through theexchanger 3′. As previously, this flow serves to cool the compressed gas to be treated, which is then discharged via theline 35. - In the same way as in the case of
FIGS. 4 and 5 , this reduces thermal fatigue effects in the exchanger. - In FIGS. 4 to 6, the apparatus furthermore includes additional heating means 13 for heating the regeneration fluid.
- This is because it may prove the case that the regeneration fluid is heated by heat exchange with the gas to be treated insufficiently for complete regeneration of an adsorber over the course of the entire adsorption/regeneration cycle. A first solution may consist in increasing the flow rate of the regeneration fluid. Alternatively or additionally to this first solution, the regenerability of the regeneration fluid may be increased by using said additional heating means 13.
- The triple-
flow exchanger 3′ replaces theexchanger 3 inFIG. 1 . - The additional heating means 13 comprise an
auxiliary heat source 14, for example an electrical heat source, linked by acircuit 15 to the hot part of theheat exchanger 3′. Thecircuit 15 forms a closed loop for the flow of a heat-transfer fluid between saidauxiliary heat source 14 and theexchanger 3′. - Means (not shown) move the heat-transfer fluid inside the
circuit 15. Advantageously, as shown, the flow of the heat-transfer fluid through theexchanger 3′ is in the opposite direction to the flow of the regeneration fluid, in order to operate as a countercurrent exchanger. - The configuration of the triple-
flow exchanger 3′ illustrated in FIGS. 4 to 6 is such that the regeneration fluid is firstly heated by countercurrent heat exchange with just the gas to be treated, in thecold part 103′ of the exchanger, and then secondly heated by countercurrent heat exchange with just the heat-transfer fluid in thehot part 203′ of the exchanger. - It will be understood that many additional changes in the details, materials, steps and arrangement of parts, which have been herein described in order to explain the nature of the invention, may be made by those skilled in the art within the principle and scope of the invention as expressed in the appended claims. Thus, the present invention is not intended to be limited to the specific embodiments in the examples given above.
Claims (15)
1. A process for treating a gas by adsorption in an adsorber comprising:
(a) compressing a gas to be treated;
(b) making the gas to be treated from step (a) flow through an adsorber in adsorption phase;
(c) making a stream of regeneration fluid flow through the adsorber in a regeneration phase;
(c1) during a first part of the adsorber regeneration phase, indirect heat exchange between the gas to be treated from step (a) and a regeneration fluid stream is established in a heat exchanger so as to cool the gas to be treated from step (a) and intended for step (b) and to heat the regeneration fluid intended for step (c), and
(c2) during a second part of the adsorber regeneration phase, the regeneration fluid is made to flow through the adsorber without making it undergo the heat exchange of step (c1);
(d) performing auxiliary refrigeration of the gas to be treated during said step (c2); and
(e) heating the regeneration fluid coming from step (c1) by means of an auxiliary heat injection before this regeneration fluid is made to pass through the adsorber.
2. The process of claim 1 , wherein said auxiliary refrigeration step (d) further comprises refrigerating the gas to be treated by an auxiliary cold source.
3. The process of claim 1 , wherein said auxiliary refrigeration step (d) further comprises refrigerating the gas to be treated by at least one part of the stream of regeneration fluid that has passed through the adsorber.
4. The process of claim 1 , wherein said auxiliary refrigeration is carried out in the heat exchanger.
5. The process of claim 1 , wherein said auxiliary refrigeration is carried out outside the heat exchanger.
6. The process of claim 5 , wherein a flow of the gas to be treated and of the regeneration fluid is maintained in the heat exchanger during said auxiliary refrigeration step (d).
7. The process of claim 1 , further comprising cooling the gas to be treated from step (c1), before this gas to be treated is made to pass through the adsorber.
8. The process of claim 1 , wherein the gas to be treated is atmospheric air, in that the function of step (b) is to strip water and carbon dioxide from the air to be treated coming from step (a), in that said process further comprises separating the air from step (b) by distillation in order to produce at least one of its constituents and also a waste gas, and in that the waste gas forms said regeneration fluid.
9. An apparatus for treating a gas by adsorption comprising:
a) a compressor or compressing a gas to be treated, the delivery side of the compressor is designed to be connected to the inlet of at least one adsorber during an adsorption phase of the latter;
b) a means for making a regeneration fluid flow through the adsorber during a regeneration phase of the latter; and
c) a means for heating the regeneration fluid entering the adsorber in regeneration mode, wherein:
1) the heating means comprises a heat exchanger designed to bring the regeneration fluid into indirect heat exchange with the gas coming from the compressor;
2) the apparatus further comprises:
i) a branch-off means for sending the regeneration fluid into the adsorber in regeneration mode without passing through the heat exchanger; and
ii) an auxiliary refrigerating means for refrigerating the gas to be treated when said branch-off means are activated; and
3) the heating means further comprises an auxiliary heat source designed to carry out additional heating on the regeneration fluid.
10. The apparatus of claim 9 , wherein the auxiliary refrigeration means comprise an auxiliary cold source for at least the cold part of the heat exchanger.
11. The apparatus of claim 9 , wherein the auxiliary refrigerating means comprise a branch-off from a circuit for gas to be treated, that branch-off being mounted across the terminals of the heat exchanger and provided with an auxiliary cold source.
12. The apparatus of claim 9 , wherein the auxiliary refrigerating means comprise a return line for returning the regeneration fluid to the heat exchanger after said fluid has passed through the adsorber in regeneration mode.
13. The apparatus of claim 9 , wherein the auxiliary heat source is designed to provide additional heat for at least the hot part of the heat exchanger.
14. The apparatus of claim 9 , further comprising an additional cooling means for cooling the gas to be treated, these means being placed between the heat exchanger and the adsorber.
15. The apparatus of claim 9 , wherein an assembly starting from the compressor to the adsorber is placed upstream of an air separation installation for producing at least one of the constituents of air by distillation, in that the adsorber is intended to strip water and carbon dioxide from the air to be treated, and in that the regeneration fluid is formed from a waste gas produced by this separation installation.
Priority Applications (1)
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US11/327,878 US20060156922A1 (en) | 2001-10-09 | 2006-01-09 | Method and apparatus for treating a gas by adsorption in particular for purifying atomspheric air |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
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FR0112968A FR2830463B1 (en) | 2001-10-09 | 2001-10-09 | METHOD AND APPARATUS FOR THE TREATMENT OF A GAS BY ADSORPTION, IN PARTICULAR FOR THE CLEANING OF ATMOSPHERIC AIR BEFORE SEPARATION BY DISTILLATION |
US10/492,491 US6984258B2 (en) | 2001-10-09 | 2002-10-09 | Method and apparatus for treating a gas by adsorption in particular for purifying atmospheric air |
US11/327,878 US20060156922A1 (en) | 2001-10-09 | 2006-01-09 | Method and apparatus for treating a gas by adsorption in particular for purifying atomspheric air |
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US10/492,491 Continuation-In-Part US6984258B2 (en) | 2001-10-09 | 2002-10-09 | Method and apparatus for treating a gas by adsorption in particular for purifying atmospheric air |
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US11/327,878 Abandoned US20060156922A1 (en) | 2001-10-09 | 2006-01-09 | Method and apparatus for treating a gas by adsorption in particular for purifying atomspheric air |
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- 2001-10-09 FR FR0112968A patent/FR2830463B1/en not_active Expired - Fee Related
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2002
- 2002-10-09 JP JP2003534052A patent/JP4234598B2/en not_active Expired - Fee Related
- 2002-10-09 AT AT02800643T patent/ATE322329T1/en not_active IP Right Cessation
- 2002-10-09 DE DE60210490T patent/DE60210490T2/en not_active Expired - Fee Related
- 2002-10-09 EP EP02800643A patent/EP1436067B1/en not_active Expired - Lifetime
- 2002-10-09 CN CNB028199146A patent/CN1255204C/en not_active Expired - Fee Related
- 2002-10-09 WO PCT/FR2002/003433 patent/WO2003031027A1/en active IP Right Grant
- 2002-10-09 US US10/492,491 patent/US6984258B2/en not_active Expired - Fee Related
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2006
- 2006-01-09 US US11/327,878 patent/US20060156922A1/en not_active Abandoned
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Also Published As
Publication number | Publication date |
---|---|
EP1436067A1 (en) | 2004-07-14 |
WO2003031027A1 (en) | 2003-04-17 |
US20040244594A1 (en) | 2004-12-09 |
DE60210490D1 (en) | 2006-05-18 |
FR2830463B1 (en) | 2004-08-06 |
DE60210490T2 (en) | 2006-12-14 |
FR2830463A1 (en) | 2003-04-11 |
US6984258B2 (en) | 2006-01-10 |
EP1436067B1 (en) | 2006-04-05 |
ATE322329T1 (en) | 2006-04-15 |
JP4234598B2 (en) | 2009-03-04 |
CN1255204C (en) | 2006-05-10 |
JP2005504627A (en) | 2005-02-17 |
CN1564704A (en) | 2005-01-12 |
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