EP2139807A2 - Ecretement des pics d'impurete - Google Patents
Ecretement des pics d'impureteInfo
- Publication number
- EP2139807A2 EP2139807A2 EP08788025A EP08788025A EP2139807A2 EP 2139807 A2 EP2139807 A2 EP 2139807A2 EP 08788025 A EP08788025 A EP 08788025A EP 08788025 A EP08788025 A EP 08788025A EP 2139807 A2 EP2139807 A2 EP 2139807A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- adsorbent
- content
- equal
- gas
- zeolite
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Ceased
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- 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
-
- 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
-
- 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
- B01D2253/30—Physical properties of adsorbents
- B01D2253/34—Specific shapes
- B01D2253/342—Monoliths
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/16—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/502—Carbon monoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/41—Further details for adsorption processes and devices using plural beds of the same adsorbent in series
-
- 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
- B01D53/047—Pressure swing adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
Definitions
- the present invention relates to a process for purifying or separating gas intended to produce a gaseous mixture containing predominantly hydrogen and a minor amount of CO, whose CO content must necessarily remain below a determined value. It relates particularly to adsorption processes and more particularly PSA (pressure swing adsorption) processes.
- PSA methods or units serve to purify or separate a gaseous feed stream. They generally comprise several adsorbers filled with selective adsorbent materials with respect to at least one of the constituents of the feed stream. These adsorbers follow a pressure modulation cycle comprising a succession of phases which define adsorption stages at the high pressure of the cycle, decompression, extraction of the most adsorbed components and recompression. Generally the arrangement of the cycle is such that production is provided continuously without the need to provide a storage capacity.
- the PSA processes treating the H 2 / CO synthesis gas operate at a given feed gas flow rate, the feed gas feedstock coming for example from a steam reforming unit of natural gas.
- a shortening of the cycle time makes it possible to obtain a purer hydrogen fraction, to the detriment of the extraction yield, that is to say of the quantity of hydrogen actually produced.
- the content of impurities varies during the production phase.
- the product gas consists of the least adsorbable compounds
- the content Yi of a given impurity i decreases very rapidly at the beginning of the production stage and increases more slowly towards the end of the same stage.
- FIG. 1 represents the content Yi in impurity in molar ppm as a function of the phase time; it ranges from a few seconds for the so-called fast PSA (RPSA) to a few minutes or tens of minutes for more conventional PSA
- RPSA fast PSA
- the high content of impurities at the beginning of the phase time is explained by the fact that the adsorber in question has just been repressurized via gas from an adsorber at the end of the production stage: the gas produced in the very first instants therefore has the composition of the gas produced at the end of the production step (mirror effect) .
- the operation of the PSA should be adapted so that the impurity content of the systematic or accidental peaks remains below the maximum value specified for the impurity in question.
- the maximum permissible CO content is 5 ppm molar
- the corresponding PSA H2 will be regulated to obtain systematic peaks in output of the order of 1 to 2 ppm, which will generally give sufficient margin to pass the periodic peaks. accidentals which can then reach 3 to 4 ppm.
- the systematic peaks correspond to CO contents of 2 to 3 times higher, whereas the periodic peaks can reach, for their part, 6 to 7 times this average value.
- the duration of these peaks for a standard H2 PSA will generally be of the order of a few seconds. More generally, they represent in duration only a small percentage of the phase time of a PSA, of the order of a few percent.
- Document FR-A-2 735 381 proposes to insert between the gas production unit and the user a reservoir containing an adsorbent material making it possible to slow down the progression of an accidental peak to allow time to analyze the production, detect the problem and torch production out of specification. Such a method allows to take less margin on the operation of the unit but only partially solves the problem. Indeed, if it avoids the pollution of the downstream circuit in CO, this system leads to stop the supply of hydrogen from the unit as soon as a peak exceeds the maximum permissible content.
- Document US Pat. No. 3,897,226 proposes to add a complementary adsorber between the gas production unit and the user and to purify with this adsorber the gas coming from the main unit as soon as the content of impurities exceeds a given threshold.
- this device makes it possible to manage accidental peaks or occurring at sufficiently long intervals of time.
- the system is complex in the sense of controlling the flow rates to the adsorber and bi-passing the adsorber to remain below the limit impurity threshold.
- GB-A-2,113,567 proposes to add in series with the main adsorption cycle an adsorber further purifying the production gas from the main unit as soon as the latter is no longer the required specification.
- This complementary adsorber is regenerated at each cycle together with one of the adsorbers of the main unit.
- This system makes it possible to trim the systematic peaks of impurities but at the cost of a major complication of the main unit. This system makes it difficult to answer the most classic case of systematic peaks at the beginning and end of the production stage.
- a number of PSAs have multiple adsorbers simultaneously in production. This is the case, for example, of H2 PSAs which deal with large gas flows, for which 2, 3, 4 or even more adsorbers simultaneously supply hydrogen.
- Each of the adsorbers having started its production cycle at a different time, the production is somehow automatically averaged. Such a system effectively decreases the relative importance of systematic or accidental peaks, but does not eliminate this effect.
- EP-A-748765 describes the installation of a tank containing an adsorbent material having an affinity for carbon monoxide between a carbon monoxide purification unit by adsorption to stop water and CO2 and a unit cryogenic separation.
- the purpose of this unit is to regulate the flow of carbon monoxide which varies cyclically: the adsorbent material supplied with CO when the production flow is reduced and stores CO in the opposite case.
- the tank acts as a storage capacity. In this case, it is a variation of the order of the% around average characteristics. On the other hand, it is not a question in this process of limiting the content of CO in pure hydrogen at the ppm level. Nor is it considered to treat fluctuations in CO content that can reach or exceed 6 to 7 times the average content in production.
- the adsorbent could be molecular sieve, in particular the same adsorbent as that used in the main purification.
- US Pat. No. 6,605,136 teaches that in order to stop the CO in hydrogen, one or more zeolites with or without a binder belonging to CaA, NaX, CaX or BaX can be selected. , LiX, NaLSX, CaLSX, BaLSX and LiLSX.
- US-A-2006/0254425 indicates that most of the CO can be preferentially adsorbed in a high density activated carbon layer but that exchanged zeolites of type A, X, Y, chabazite, mordenite, etc. can be used. It also teaches that the residual CO content will advantageously be stopped by zeolites of the CaA, LiX, CaX, LiLSX, CaLSX, Li-mordenite or Ca-mordenite type, etc. It is specified that adsorbents having a Henry constant for CO greater than 2.94 (mmol / g) / bar are preferred. It is also specified that a material having a Henry's constant greater than 10 (mmol / g) / bar adsorbs too strongly the compound to be stopped for use in a PSA.
- a solution of the invention is a process for purifying or separating a feed gas stream containing hydrogen H 2 and a carbon monoxide (CO) molar content greater than or equal to 1000 ppm, in which a) said stream of feed gas is introduced continuously into a first PSA purification unit (10) containing a first adsorbent on which CO is preferentially adsorbed; b) recovering the gas from step a) at least partially purified by CO and having an average molar CO content T, less than or equal to Tacc, itself being less than or equal to 100 ppm, and punctually a first maximum TMo content in CO higher than Tacc, c) is introduced continuously all of the gas from step b) in a downstream adsorber (20) containing at least a second adsorbent (21) on which CO is preferentially adsorbed; d) recovering the H2 enriched gas from step c) having a mean CO content T and a maximum TMi content of CO both less than or equal to Tacc.
- Tacc is the acceptable CO content by the downstream process.
- Tacc is preferably less than 50 ppm, more preferably less than 25 ppm and more preferably less than 10 ppm.
- the method according to the invention may have one of the following characteristics:
- the maximum TMi content in CO is such that (TMi - T) ⁇ / 4 (TMo - T), preferably (TMi - T) ⁇ 1/5 (TMo - T), preferentially still (TMi - T) - T) ⁇ 1/10 (TMo - T); in step b) the maximum TMo content in CO is such that TMo ⁇ 1.1 x T, preferably TMo> 2 x T.
- the second adsorbent exhibits at 20 ° C., an Henry's constant for CO greater than or equal to 2.5 (mmol / g) / bar, preferably greater than or equal to 5 (mmol / g); bar; the first and second adsorbents are either identical or different when the second adsorbent has a lower adsorption kinetics than that of the first adsorbent;
- the second adsorbent is of granular type, in particular in the form of beads or rods, whereas the first adsorbent is of monolithic type, in particular in the form of sheets;
- the second adsorbent is chosen from an X zeolite, preferably an LSX zeolite, a 5A zeolite or an exchanged zeolite, in particular a zeolite exchanged with more than 50%;
- the downstream adsorber contains at least two different adsorbent materials;
- the feed gas stream is obtained by steam reforming, by partial oxidation of hydrocarbons or alcohols, by gasification of the coal or residues, or by mixed processes;
- the gas resulting from step d) is intended for a pipe-type network A, a chemical-petrochemical unit, a unit forming part of a refinery or the feed of a fuel cell.
- the unit 10 represents a unit for purifying the feed gas 1.
- This unit is for example a hydrogen PSA treating a flow rate of charge of 165,000 NmVh of a gas resulting from a reforming with steam, at a pressure of 20 bar abs, a temperature of 35 ° C. and having a composition corresponding to 70% mole H 2 , 22% CO 2 , 4% CH 4 , 4% CO (dry gas).
- This purification unit 10 virtually eliminates CO 2 , CH 4 and CO.
- the adsorbent used as the last bed to stop CO is a commercial adsorbent type 5A, available from suppliers such as UOP, CECA, ZEOCHEM.
- the production flow 2 of this unit consists of just over 100,000 Nm / h of hydrogen with a residual carbon monoxide content regularly varying between 0.5 and 1.5 ppm and periodically having peaks around 3 to 4 ppm.
- This production 2 is introduced completely and continuously into a downstream adsorber 20 containing a second adsorbent 21.
- the fluid 3 has a substantially constant CO content around 0.8 ppm, remaining in practice in a range of 0.75 / 0.85 ppm.
- Figure 5 shows that the downstream adsorber 20 containing the second adsorbent 21 acts as a clipper with respect to impurity peaks.
- a first curve A gives the content of impurities in molar ppm of the flow of gas entering the adsorber 20 over time in minutes;
- a second curve B gives the content of impurities in molar ppm of the gas flow leaving the adsorber 20 over time in minutes and
- a third curve C gives the average impurity content in molar ppm of the outgoing or incoming gas flow of the adsorber 20 over the time in minutes. From there, we see that the curve B does not present the amplitude in ordinate of the curve A and tends to approach the curve C.
- the CO will pass more or less quickly from the adsorbed phase to the gas phase.
- This transfer delay between the two phases allows spreading of the impurity peak.
- a too low adsorption kinetics will disadvantage peak spreading in the sense that the impurity peak will move through the adsorbent without the CO being adsorbed: the peak will then be slightly deformed.
- the CO peak will be instantly adsorbed and released. The delay effect of the adsorbent will then be reduced and the spread of the peak will be less.
- the method according to the invention makes it possible, without fear of pollution, to reduce the margins taken in the state of the art on the operation and to adjust the PSA implemented in step a) to produce hydrogen with a average 0.8 molar CO content is 3 to 4 times higher than the initially planned setting - of the order of 0.2 ppm - without the addition of the downstream adsorber 20.
- Such a modification makes it possible to produce about 500 Nm / h additional or to reduce the necessary feed rate, ie the consumption of natural gas while more surely respecting the condition on the maximum CO content.
- a small volume of adsorbent 21 is sufficient to average the impurity content of the gas very efficiently from the moment when the adsorbent is chosen wisely. In the case of the example, just a few m 3 of adsorbent is sufficient to smooth the production of a PSA producing more than 100,000 NmVh of hydrogen.
- the first tests consisted in determining the Henry constants of various adsorbents including those conventionally used in the PSA for the cessation of CO
- the Henry's constant is indeed a good parameter to characterize the adsorption.
- Dimensional impurity means the impurity whose shutdown at the required level determines the performance of the adsorption unit. In this case, it is the CO.
- the Henry's constant is the ratio of the adsorption capacity Q to the adsorption pressure P when said pressure P tends to 0.
- the initial state of the adsorbent is critical for the adsorption of traces, the samples are regenerated from 350 ° to 450 0 C according to the type of zeolite in a vacuum of 10 "mbar for 8 hours.
- H A.
- the unit selected for H is (mmol / g) / bar, that is to say milli-mole of CO adsorbed per gram of adsorbent and per bar.
- the zeolites tested are commercial zeolites essentially from UOP, CECA, ZEOCHEM, AXENS ....
- the adsorbents of the Heulandite, Chabazite or Mordenite type having a low Si / Al ratio, that is to say less than 10, are suitable for the process according to the invention.
- zeolites X which correspond to a faujasite type structure whose Si / Al ratio is less than 1.5. It is well known in the literature that by varying the Si / Al ratio from 1 (in this case the structure is known as LSX) to 1.5, the Henry's constant can be varied continuously. The type of cation can also play a major role on Henry's constant, for example for the family of zeolites A (LTA) the ratio Si / Ai is fixed and equal to 1, the variations of the observed Henry's constant come from the nature of the cations present.
- LTA family of zeolites A
- the adsorbent is first swept with pure hydrogen under the operating conditions chosen, in this case bar abs and 20 ° C., then the input composition is changed as quickly as possible, here introducing a few tens of ppm of CO in hydrogen keeping constant the other operating conditions (pressure, temperature).
- the OC breakthrough curve is recorded and then simulated using an appropriate simulation program.
- the program used for the simulation is based on the principles of mass conservation (including axial dispersion), enthalpy conservation (non-isothermal), momentum conservation and uses the Fick model (see “ Principles of adsorption and adsorption processes ", John-Wiley & Sounds, 1984; DM Ruthven; or "Gas Separation by Adsorption Processes", Butterworth, 1987, Ralph T. Yang), not simplified to the LDF formula (Linear Driving Force), for the fine evaluation of the kinetics of solid-gas transfers within the mass of adsorbent.
- the kinetic coefficient K (s " ) is adjusted, using the program described above, until the simulation and the experimental curve are in agreement.Experimental breakthroughs are made for several flow rates of increasing importance. In this way, it is ensured that it is really a kinetics linked to the adsorbent and not to a film resistance due to a too low circulation speed through the bed. This film resistance could be taken into account by a model implemented in the simulation but the accuracy on the intrinsic kinetics would then be lower.
- experimental conditions such as the resistance to the transfer of material through the external film of the ball is negligible, it is seen by using particles of different size of the same product that the main resistance is of macropore type, that is to say that the kinetics varies inversely proportional to the square of the diameter of the particle.
- the adsorbent will generally be in the form of wound sheets impregnated with zeolite crystals, in the form of fabric, more generally in the form of monolith with equivalent diameters of the order or less than 0.1mm.
- the kinetics used in the RPSA is between 5 and 1000 times faster than that of the classic H2 PSA.
- the characteristic dimension of a particle is defined as the diameter of the sphere having the same volume as the particle in question. Other definitions exist but lead to more complex mathematical expressions.
- the characteristic dimension D or equivalent diameter of a ball is that of the sphere of the same dimension, whereas that of a cylindrical particle (pellet or extruded e.g.) of diameter d and length or height 1 is such that:
- the spreading factor was defined here as the ratio of the residual difference in the adsorber outlet to the initial difference.
- the spreading factor is thus expressed as follows:
- the kinetics was kept constant and corresponds to the kinetics measured on a commercial 13X zeolite with a diameter equivalent to 1.6 mm. In practice, this kinetics corresponds to industrial adsorbents used in H2 PSAs with equivalent diameters in the range 1.4 to 2.1 mm.
- the reference H / 3 corresponds to a 13 X zeolite (Henry constant of 2.23 (mmol / g) / bar50), the reference H to a zeolite having an Henry constant of 6.69 (type 5A) and the reference 3H to a constant Henry of 20 (CaX or LiLSX).
- Table 1 Spread factor of a peak of 10 ppm CO as a function of Henry's constant and constant kinetic adsorber length
- adsorbents with a Henry constant high or very high can significantly reduce the length, ie the volume of adsorbent to use.
- K kinetics were varied by more than an order of magnitude, which corresponds in practice to using particles 1 to 5 mm in diameter equivalent.
- K / 3 and K / 9 two slower kinetics (K / 3 and K / 9) and faster kinetics (3K) were tested.
- the kinetics referenced K / 3 corresponds to an adsorbent of equivalent diameter in the approximate range 2.5 / 3.5 mm.
- Table 2 spreading factor of a peak of 10 ppm of CO as a function of the kinetics and the length of the adsorber (case of a zeolite X)
- Table 3 spreading factor of a peak of 10 ppm of CO depending on the kinetics and the length of the adsorber (case of a zeolite 5A)
- Table 4 spreading factor of a peak of 10 ppm of CO as a function of the kinetics and the length of the adsorber (case of a CaX / LiLSX zeolite)
- the preferred adsorbent for the downstream adsorber 20 will be an adsorbent with a constant Henry equal or greater than that recommended for adsorbent PSA, preferably greater than 5.5 (mmol / g) / bar and with kinetics equal to or less than that of the PSA adsorbent.
- PSA adsorbent means the adsorbent (s) intended to stop the CO, that is to say in particular the adsorbent constituting the last layer of the bed in a PSA H2 treating a synthesis gas ...
- FIG. 4 shows a graph representing the spreading factor on the ordinate and the kinetic coefficient of the shortest adsorption bed (reference L / 3) on the abscissa.
- an adsorbent with an Henry constant equal to or greater than that of the PSA adsorbent and with a much lower kinetics will preferably be used as the adsorbent for the downstream adsorber.
- particles, beads or rods will preferably be used, even if the adsorbent of the RPSA is in the form of a monolith.
- the downstream adsorber 20 will preferably be of the standard type, ie cylindrical with a vertical axis, with a flow from top to bottom.
- the adsorbent filler can be retained between two inert bead beds of small thickness favoring the gas distribution within the adsorbent.
- adsorbers may be used as radial adsorber or cylindrical adsorber horizontal axis depending on the amounts of adsorbant to be installed and the operating conditions.
- the installation may comprise a particle filter incorporated or not in the downstream adsorber 20, loss of pressure measurements and isolation means to intervene if necessary on the downstream adsorber 20. If necessary, in case of large and periodic peaks, it is possible to create residence times of different duration in the downstream adsorber 20. It suffices for this purpose for example to use two types of adsorbent materials of different characteristics and / or offering the feed gas 2 paths of different length. Some embodiments are shown in Figure 3.
- the adsorber 3a in which the adsorbent is deposited on an inclined grid offers the gas of different paths.
- the adsorber 3b is filled with 2 different materials separated by an inclined grid.
- the two adsorbents will have a common particle size. The local speeds will then be identical in the same section.
- One of the two adsorbents may be a zeolite 3A inert with respect to CO.
- the adsorber 3c contains concentric cylinders. The spaces between the cylinder are filled with different adsorbents or with the same adsorbent but at different heights. From there, one can design various adsorption systems combining materials and / or different paths to promote the clipping of impurity peaks. It goes without saying that such systems are more complex to size than a single adsorbent bed and will be used only if a simple clipping via a conventional adsorber is insufficient.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0753986A FR2913969B1 (fr) | 2007-03-22 | 2007-03-22 | Ecretement des pics d'impurete |
PCT/FR2008/050478 WO2008132377A2 (fr) | 2007-03-22 | 2008-03-20 | Ecretement des pics d'impurete |
Publications (1)
Publication Number | Publication Date |
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EP2139807A2 true EP2139807A2 (fr) | 2010-01-06 |
Family
ID=38646755
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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EP08788025A Ceased EP2139807A2 (fr) | 2007-03-22 | 2008-03-20 | Ecretement des pics d'impurete |
Country Status (5)
Country | Link |
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US (1) | US8202351B2 (fr) |
EP (1) | EP2139807A2 (fr) |
CN (1) | CN101641283B (fr) |
FR (1) | FR2913969B1 (fr) |
WO (1) | WO2008132377A2 (fr) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
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DE102008052874A1 (de) * | 2008-10-23 | 2010-04-29 | Linde Aktiengesellschaft | Druckwechseladsorptionsverfahren |
FR2991192A1 (fr) * | 2012-06-04 | 2013-12-06 | Air Liquide | Procede de production d'hydrogene a differents niveaux de purete par un psa h2 |
FR3069786A1 (fr) * | 2017-08-03 | 2019-02-08 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de production d'un flux gazeux d'hydrogene haute purete |
FR3069787B1 (fr) * | 2017-08-03 | 2019-08-09 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de production continue d'un flux gazeux d'hydrogene |
US10882004B2 (en) * | 2018-08-23 | 2021-01-05 | Uop Llc | Reducing peak compositions in regeneration gas for swing adsorption processes |
KR20210089681A (ko) * | 2018-11-19 | 2021-07-16 | 스미토모 세이카 가부시키가이샤 | 가스 분리 장치 및 가스 분리 방법 |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
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GB1431767A (en) | 1972-04-19 | 1976-04-14 | Petrocarbon Dev Ltd | Controlling the concentration of impurities in a gas stream |
JPS58128123A (ja) | 1982-01-26 | 1983-07-30 | Taiyo Sanso Kk | ガスの分離方法とその装置 |
JPH04502581A (ja) * | 1989-10-27 | 1992-05-14 | ポール・コーポレーション | 気体からの成分を収着する装置および方法 |
FR2735381B1 (fr) * | 1995-06-15 | 1997-07-25 | Air Liquide | Installation de fourniture d'un gaz incorporant un dispositif de detection d'impuretes |
FR2735382B1 (fr) | 1995-06-15 | 1997-07-25 | Air Liquide | Installation de production de monoxyde de carbone incorporant une unite de separation cryogenique |
FR2806072B1 (fr) * | 2000-03-07 | 2002-06-07 | Air Liquide | Charbon actif ameliore par traitement a l'acide et son utilisation pour separer des gaz |
US6605136B1 (en) * | 2002-07-10 | 2003-08-12 | Air Products And Chemicals, Inc. | Pressure swing adsorption process operation and optimization |
AU2003299775A1 (en) * | 2002-12-24 | 2004-07-22 | Praxair Technology, Inc. | Process and apparatus for hydrogen purification |
US7404846B2 (en) * | 2005-04-26 | 2008-07-29 | Air Products And Chemicals, Inc. | Adsorbents for rapid cycle pressure swing adsorption processes |
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2007
- 2007-03-22 FR FR0753986A patent/FR2913969B1/fr active Active
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2008
- 2008-03-20 CN CN200880009351.1A patent/CN101641283B/zh active Active
- 2008-03-20 US US12/532,171 patent/US8202351B2/en active Active
- 2008-03-20 WO PCT/FR2008/050478 patent/WO2008132377A2/fr active Application Filing
- 2008-03-20 EP EP08788025A patent/EP2139807A2/fr not_active Ceased
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Also Published As
Publication number | Publication date |
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CN101641283A (zh) | 2010-02-03 |
CN101641283B (zh) | 2013-01-16 |
FR2913969A1 (fr) | 2008-09-26 |
WO2008132377A2 (fr) | 2008-11-06 |
WO2008132377A3 (fr) | 2009-02-05 |
US20100071551A1 (en) | 2010-03-25 |
US8202351B2 (en) | 2012-06-19 |
FR2913969B1 (fr) | 2010-02-19 |
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