WO2005000447A1 - Procede de prepurification d'air par cycle tsa accelere - Google Patents
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- WO2005000447A1 WO2005000447A1 PCT/FR2004/050283 FR2004050283W WO2005000447A1 WO 2005000447 A1 WO2005000447 A1 WO 2005000447A1 FR 2004050283 W FR2004050283 W FR 2004050283W WO 2005000447 A1 WO2005000447 A1 WO 2005000447A1
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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
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0431—Beds with radial gas flow
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/104—Alumina
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
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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
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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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
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
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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
- B01D2259/40007—Controlling pressure or temperature swing adsorption
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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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/4006—Less than four
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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
- B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
- B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
- B01D2259/4145—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged in series
- B01D2259/4146—Contiguous multilayered adsorbents
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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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the present invention relates to a TSA process for the prepurification of air intended to be subsequently fractionated by cryogenic means.
- the air to be distilled by cryogenic means is previously dried, decarbonated and at least partially freed from the secondary atmospheric pollutants which it contains, such as hydrocarbons, nitrogen oxides or the like, by passing the air through one or more adsorbent masses arranged in one or more adsorption zones of an air prepurification unit.
- This process is commonly called the air prepurification process or more simply the overhead cleaning process.
- the main object of such a prepurificatjon is to stop and eliminate the various atmospheric impurities likely to be present in the gas flow, until obtaining contents compatible with the good functioning of the cryogenic unit supplied with this air, whether in terms of performance or equipment safety.
- a prepurification process can use a single or more adsorbent beds, located in one or more adsorbers, commonly called adsorption bottles.
- the adsorbents used to remove these impurities are in particular exchanged or non-exchanged zeolites, silica gels, activated and / or doped aluminas, or their combinations or mixtures.
- Certain adsorbents can contain, in addition to the active phase, a more or less significant quantity of binder, making it possible in particular to reinforce the mechanical resistance of the adsorbent particle, such as its resistance to attrition.
- Industrial adsorbents are generally used in the form of balls, more or less spherical, ovoid or ellipsoidal, or sticks, such as extrudates, or even more complex shapes.
- the diameter of these beads is generally between 1.5 and 4 mm and preferably between 2 and 3 mm.
- Certain particles are formed from a mixture of several adsorbents, for example a mixture of several compounds of the same nature, such as a mixture of a Nax zeolite with a NaLSX or CaX zeolite, a X zeolite with a A zeolite, or formed from several compounds of different natures, such as a mixture of a zeolite with an activated alumina.
- an adsorption bed can be formed of a single type of adsorbent or of several distinct adsorbents either distributed in juxtaposed or superposed layers, or in intimate mixture and this, in variable proportions.
- the adsorbers can be, depending on the case, with a vertical or horizontal axis, or alternatively of the radial type, that is to say that the flow of gas to be purified flows therein either vertically (from bottom to top), horizontally (from right to left, or vice versa), either centripetally (radially towards the axis of the adsorber) or centrifugal (radially away from the axis).
- the mass of adsorbent is cyclically regenerated within the adsorber itself by heating and / or gas sweeping, before being used again in the adsorption phase.
- PSA Pressure Swing Adsorption
- a TSA process cycle of air prepurification comprises the following stages: a) supply of air to an adsorber and purification of the air by adsorption of the impurities at super-atmospheric pressure and at temperature close to ambient, that is to say typically between 0 ° C. and 40 ° C. approximately, b) depressurization of the adsorber up to the pressure of the regeneration gas, generally atmospheric, c) regeneration of the adsorbent at a pressure lower than the adsorption pressure, in particular by a waste gas, typically impure nitrogen at atmospheric pressure originating from the air separation unit and heated to a higher temperature at room temperature by means of one or more heat exchangers.
- the regeneration gas is at a pressure substantially higher than atmospheric pressure due to the upstream process, for example due to pressure distillation, the regeneration gas being used downstream of the regeneration, for example recompressed.
- a short phase can be envisaged during which a regeneration step will be carried out by lowering the pressure of the regeneration gas to atmospheric pressure.
- the nitrogen in the air is adsorbed on the adsorbent (s) causing the gas contained in the adsorber to heat up during the repressurization phase.
- the rise in temperature will depend on the quantity of energy released by the nitrogen addition, therefore by the quantity of nitrogen adsorbed, itself dependent on the conditions of regeneration and absorption.
- f) inversion of the adsorbers At this stage, the energy contained in the form of heat in the adsorber is evacuated with the air flow, causing a momentary rise in temperature at the outlet of the adsorber (temperature peak). The amplitude and duration of this temperature peak depends on the amount of energy stored during the repressurization phase as well as on the air flow rate passing through the adsorber.
- the prepurification unit can be preceded by a step of possible pre-cooling of the air to be purified by means, for example, of one (or more) cold water exchanger, mechanical refrigeration unit or any other similar system.
- a PSA process cycle for air purification comprises, for its part, substantially the same steps a), b) and e), but is distinguished from a TSA process by an absence of heating of the waste gas (es) during the regeneration step (step c), and therefore also by an absence of step d).
- the regeneration can be carried out at a pressure substantially different from atmospheric pressure, either higher as already mentioned (generally in the case of ASD), or even lower than the latter.
- the waste gas can be a gas very enriched in oxygen, in the case where the recovered product of the air separation unit is nitrogen, since, in this case, the oxygen is a waste product Not used.
- the air pretreatment devices comprise two adsorbers, operating in alternating fashion, that is to say that one of the adsorbers is in the production phase, while the other is in the regeneration phase.
- TSA air purification methods are described in particular in documents US-A-3,738,084 and US-6,093,379.
- the cycle time is defined as the sum of the durations of the addition and regeneration stages.
- the addition time is equal to half the cycle time.
- the adsorption time in a PSA cycle is of the order of 3 to 30 minutes, while in a TSA cycle, it is of the order of 2 to 8 hours.
- the volume of adsorbent used in a PSA cycle is generally lower than in an TSA cycle because the effect of the reduction of the cycle, that is to say the least amount of impurities to be stopped per phase, l prevails over the fact that the regeneration of the adsorbent is only partial, which is equivalent to a lower capacity for stopping impurities.
- the PSA does not require either a heater or a cooler because the regeneration is carried out by sweeping at ambient temperature.
- the desorption energy is very generally supplied in the form of heat conveyed within the adsorbent by the regeneration gas heated beforehand.
- the quantity of gas required is then significantly lower, of the order of 5 to 25% of the gas flow rate to be treated depending on the temperature level adopted and the details of the cycle. It can be seen that the choice between PSA and TSA is generally made on the quantity of regeneration gas available. From there, the air separation units intended to produce a high percentage of valued products, i.e. oxygen, medium pressure and low pressure nitrogen ... will have little residual gas, typically low pressure impure nitrogen, and will therefore necessarily be provided with an overhead purification of the TSA type.
- the volumes to be depressurized and then to be re-pressurized are not proportional to the volume of adsorbent because a non-negligible, even preponderant, part consists of 'dead' volumes located at the bottom of the adsorbers and in the pipes up to '' to the isolation valves.
- a non-negligible, even preponderant, part consists of 'dead' volumes located at the bottom of the adsorbers and in the pipes up to '' to the isolation valves.
- document EP-A-766989 proposes heating only part of the adsorbent bed thanks to a partial PSA type operation.
- document EP-A-815920 describes the introduction of a heat pulsation in the intermediate part of the adsorber.
- document EP-A-884085 proposes a method which implements internal heating of the adsorbent.
- the problem which arises is to improve the known air prepurification processes so as to substantially reduce the prepurification cycles by TSA process, in particular the cycle time, and the volume of adsorbent ( s) to be implemented, while retaining both a simple and inexpensive heating system, that is to say by using a standard electric or steam heater and a regeneration rate compatible with the required productions of pure products , that is to say oxygen, nitrogen and / or argon.
- the solution of the invention is then a process of air prepurification by adsorption using two adsorption containers operating in parallel, alternately and in TSA cycle, each container containing at least one adsorbent arranged in at least one bed.
- each additive cycle comprising at least: a) an additive step during which at least a portion of the impurities contained in the air is removed by adsorption on said adsorbent, at an additive temperature (Tads) , the air passing through the adsorption bed in a centripetal manner, b) a regeneration step during which the adsorbent used in step a) is regenerated by sweeping with a regeneration gas at a regeneration temperature (Treg), such as Treg> Tads, the regeneration gas passing through the adsorption bed in a centrifugal manner, so as to desorb the impurities adsorbed in step a), c) a step of cooling the adso rbant during which there is a reduction in the temperature of the adsorbent having been regenerated in step b), characterized in that: - in step a), the adsorption time (Tads) is between 60 and 120 minutes, - in steps b), and optionally in step
- the method of the invention may include one or more of the following technical characteristics: - before sending the regeneration gas to an adsorber to be regenerated during a step b), an operation is carried out.
- at least one heating parameter chosen from the group formed by the heating time, the temperature level and the flow rate of the regeneration gas is controlled so that the maximum temperature at the outlet of each adsorber is lower than minus 30 ° C at the inlet temperature of the adsorber under consideration, preferably at least 60 ° C, preferably at least 90 ° C.
- the regeneration gas is nitrogen or a gas rich in nitrogen.
- the regeneration gas includes a step of filtration of the gas produced by means of a filtration means located downstream of the adsorbers.
- at least one heat exchanger is used to heat the regeneration gas and at least one bypass circuit arranged so as to allow a bypass of the heat exchanger.
- a faujasite zeolite of the LSX type without binder is used as an adsorbent.
- the regeneration flow is between 20 and 30% of the additive flow.
- the adsorption time is between 90 and 120 minutes.
- the reduction in thermal inertia is obtained by using one or more adsorbers 1 of the radial type with centrifugal circulation of the regeneration gas, that is to say from the center of the adsorber 1 towards the periphery , and with, on the other hand, centripetal circulation of the air to be purified, that is to say from the periphery towards the center of the adsorber 1, as shown diagrammatically in FIG. 1 appended, which is a view in transverse section of an adsorber 1 of axis AA, usable within the framework of the present invention.
- the air to be purified under pressure is introduced, via a first orifice 10 located in the bottom 12 of the adsorber 1, on the side of the outer peripheral wall 2 of the adsorber containing the adsorbent arranged in a bed 3 of three-dimensional cylindrical shape with hollow central volume 16, that is to say that the air to be purified is sent to the level of the external lateral periphery 8 of the bed 3 of adsorbent.
- the adsorbent particles constituting the adsorbent bed 3 are retained by two lateral grids 4, 5 perforated with gas passage orifices, situated on either side of the bed 3 of addition so as to keep the particles of said bed 3 in their initial position during the life of the equipment.
- the bed 3 rests on a support structure 6 of flat, curved or other shape as appropriate.
- the air passes through, in a centripetal manner, successively the grid 5, the bed 3 of adsorbent and the grid 4 until it reaches the center 16 of the adsorber 1.
- the impurities present in the air flow at the temperature d adsorption typically between 5 and 50 ° C. are adsorbed, during the adsorption phase, on the adsorption bed 3 which is formed of one or more adsorbents, preferably bed 3 contains a layer of alumina and a layer of zeolite, in particular of the faujasite type, in particular a zeolite X or LSX exchanged or not with metal cations.
- the type of zeolite to be used is chosen according to the impurities to be removed.
- the purified air is recovered at the center 16 of the adsorber 1 and is evacuated to a place of storage or use, via a second orifice 9 located at the level of the ceiling 11 of the adsorber 1.
- the adsorber 1 is regenerated by introducing a regeneration gas at a temperature higher than the adsorption temperature, for example nitrogen at a temperature of 50 to 250 ° C, the gas regeneration being introduced into the adsorber 1 through the second orifice 9 and passes through the bed 3 in a centrifugal manner, that is to say that it is introduced into the center 16 of the adsorber and then sweeps the bed 3 of adsorption in the direction of the external wall 2, before being discharged through the first orifice 10.
- the regeneration gas becomes charged with impurities, said impurities being desorbed from the bed 3 on which they were trapped during the previous adsorption step.
- the hot regeneration gas is no longer in contact with the wall 2 of the external envelope of each adsorber 1, which is intended to withstand the pressure mechanically, and the internal metallic mass upstream of the or beds 3 of adsorbents can be reduced significantly.
- the heating circuit 15 it is possible to keep the heating circuit 15 warm, for example by leaving the steam inlet open or more generally by keeping the heating means whatever it is at an adequate level, and possibly by creating a small circulation of fluid through this heater 13 and the connection to the adsorbers 1.
- an energy control system should be installed in order to adjust the heating to what is strictly necessary.
- the maximum temperature obtained at the outlet can be significantly lower than the regeneration temperature at the adsorber inlet. This difference depends on the adsorption and regeneration conditions (ie temperature and pressure) but it is generally at least 20 ° to 30 ° C.
- Another advantage of using a bed with a radial configuration, in this case, is that the heat losses are reduced to a minimum since the heat front circulating from the inside to the outside is not in contact with the external walls. when heating the adsorbent.
- the cooling must also be limited compared to what is conventionally done, and all the more so since the adsorber will be provided with an internal isolation device, which will reduce the possibility of heat loss by unnecessary heating of the metal constituting the structure, in particular the walls, of the adsorber.
- the heat of addition of the water increases the air temperature appreciably (temperature variation of 10 ° C for example), which implies that the addition of the C0 2 does not happen at the air inlet temperature but at a sum corresponding to this temperature increased by the effect of the heat of addition of water.
- the heat front moves faster than the material fronts, it can be shown that it suffices to cool the beds to a temperature equal to or moreover even above this sum of temperatures to obtain identical performance.
- the final cooling is effected by means of the gas to be treated itself.
- the continuous improvement of the adsorbents also makes it possible to reduce the thermal capacity of the bed for a given quantity of impurities adsorbed. Therefore, preferentially, the adsorbents developed specifically for this type of purification are used.
- the mass transfer zone that is to say the mass of adsorbent in which it there is no equilibrium between the concentrations of gas phases and adsorbed phases, becomes increasingly important and it is then possible to reduce the volume of this mass transfer zone by using adsorbents of smaller equivalent diameter.
- the choice of the size of the balls, the geometry of the adsorber ... is part of the normal work of optimizing the unit and takes into account both investment and energy Reducing the flow of regeneration and therefore the reduction of the cycle time also involves optimizing the depressurization and repressurization stages.
- the regeneration rate may not be constant for the duration of the regeneration. For example, one can have a higher flow rate during the cooling phase than during the heating phase.
- valves with ramp for opening and / or closing and on the cold box side of the cryogenic distillation unit located downstream an advanced regulation system playing on the various liquid and gaseous storages to erase or at least flatten the flow disturbances.
- the process of the present invention makes it possible to carry out TSA cycles of duration less than or equal to 240 minutes, that is to say with an adsorption phase less than or equal to 120 minutes, while not requiring only regeneration flows of less than 35%, or even 30% of the air flow, which does not allow, for the same application, to use a PSA type cycle.
- Comparative example A comparison was made between a conventional ASD cycle with overhead beds, with thermal inertia and current inversion time, that is to say ranging from approximately 30 minutes for the longest cycles to 15 minutes for the longest cycles. short cycles, and an accelerated cycle TSA unit according to the invention, according to the principle of FIGS. 1 and 2.
- the regeneration flows indicated as a percentage of the air flow to be purified are obviously depending on the operating conditions, the internal dimensioning rules specific to each installation considered, the technologies used, the quality of the insulation, the layout, the type of heater ..., but the very mechanism of the comparison remains general and helps to understand the different effects.
- the TSA cycle is an air cleaning cycle for which the addition stage is carried out at 6 bar abs and at 25 ° C. Table I below gives for different durations of addition the necessary regeneration flow expressed in% of the air flow. Table I
- test E was carried out by introducing, in addition, a shortening of 30% of the transient stages, essentially of the depressurization stage (high flow rate made possible by the radial solution), a system of advanced regulation of the type described in document EP-A-1080773 and improved cooling, that is to say limited to temperature due to the adsorption of water.
- the results of tests D and E are given in Table II below; test C given for comparison. Table II
- the process of the invention therefore proves to be advantageous on 'short' or 'very short' cycles, that is to say those of 120 minutes to 60 minutes, respectively, but it must be emphasized that it can be also be for longer cycles, in particular up to 180 minutes or more, because it reduces the regeneration rate and produces a maximum amount of purified air.
- 'radial' adsorbers that is to say with adsorbent bed arranged in the shape of a three-dimensional cylinder, allows great flexibility in dimensioning because, on the one hand, it overcomes the constraints of speed limit, which makes it possible to reduce the passage sections offered to the gases in circulation and, on the other hand, it also makes it possible to install large passage sections associated with thin beds if it is desired to favor the reduction of pressure drops and thereby energy.
- TSA unit sizes of 'radial' types according to the invention capable of ensuring the purification of a high air flow, namely a flow of 860,000 Nm3 / h at a pressure of 7.5 bars abs.
- the implementation of certain aspects of the process of the invention makes it possible to reduce the regeneration rate and thereby the given available regeneration rate cycle time.
- the adsorbent beds are necessarily thin and for large air flow rates to be purified, that is to say of the order of at least 100,000 Nm 3 / h, the adsorbers will be difficult to industrialize and will present significant dead volumes, ie that they will be “cheese box” type adsorbers. Rather, spherical or preferably cylindrical adsorbers with a horizontal axis will be used.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/560,054 US20060254420A1 (en) | 2003-06-27 | 2004-06-18 | Method for prepurifying air in an accelerated tsa cycle |
EP04767845A EP1638669A1 (fr) | 2003-06-27 | 2004-06-18 | Procede de prepurification d'air par cycle tsa accelere |
JP2006516354A JP2007516059A (ja) | 2003-06-27 | 2004-06-18 | 促進されたtsaサイクルにおいて空気を予備精製するための方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0307794A FR2856607B1 (fr) | 2003-06-27 | 2003-06-27 | Procede de purification d'air par cycle tsa accelere |
FR03/07794 | 2003-06-27 |
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WO2005000447A1 true WO2005000447A1 (fr) | 2005-01-06 |
WO2005000447A8 WO2005000447A8 (fr) | 2005-03-10 |
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PCT/FR2004/050283 WO2005000447A1 (fr) | 2003-06-27 | 2004-06-18 | Procede de prepurification d'air par cycle tsa accelere |
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US (1) | US20060254420A1 (fr) |
EP (1) | EP1638669A1 (fr) |
JP (1) | JP2007516059A (fr) |
CN (1) | CN1812827A (fr) |
FR (1) | FR2856607B1 (fr) |
WO (1) | WO2005000447A1 (fr) |
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EP2803401A1 (fr) | 2013-05-16 | 2014-11-19 | Air Products And Chemicals, Inc. | Purification de l'air |
US20220065530A1 (en) * | 2019-02-21 | 2022-03-03 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | System and method for separating air gases at low pressure |
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FR2909899A1 (fr) * | 2006-12-14 | 2008-06-20 | Air Liquide | Adsorbeurs radiaux installes en parallele |
FR2911077B1 (fr) * | 2007-01-05 | 2009-11-27 | Air Liquide | Procede de purification ou de separatiion utilisant plusieurs adsorbeurs decales en phase |
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- 2004-06-18 CN CNA2004800182555A patent/CN1812827A/zh active Pending
- 2004-06-18 WO PCT/FR2004/050283 patent/WO2005000447A1/fr not_active Application Discontinuation
- 2004-06-18 EP EP04767845A patent/EP1638669A1/fr not_active Withdrawn
- 2004-06-18 US US10/560,054 patent/US20060254420A1/en not_active Abandoned
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EP1080773A1 (fr) * | 1999-09-03 | 2001-03-07 | L'air Liquide Société Anonyme pour l'étude et l'exploitation des procédés Georges Claude | Procédé et système de purification d'air à régénération thermique |
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EP2803401A1 (fr) | 2013-05-16 | 2014-11-19 | Air Products And Chemicals, Inc. | Purification de l'air |
US9108145B2 (en) | 2013-05-16 | 2015-08-18 | Air Products And Chemicals, Inc. | Purification of air |
US20220065530A1 (en) * | 2019-02-21 | 2022-03-03 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | System and method for separating air gases at low pressure |
Also Published As
Publication number | Publication date |
---|---|
FR2856607B1 (fr) | 2006-08-18 |
WO2005000447A8 (fr) | 2005-03-10 |
JP2007516059A (ja) | 2007-06-21 |
FR2856607A1 (fr) | 2004-12-31 |
EP1638669A1 (fr) | 2006-03-29 |
CN1812827A (zh) | 2006-08-02 |
US20060254420A1 (en) | 2006-11-16 |
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