Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/02—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
• • 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
  • 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
• • 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
• • 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
  • B01D53/0476—Vacuum pressure swing adsorption
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
  • B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
  • B01J20/16—Alumino-silicates
  • B01J20/18—Synthetic zeolitic molecular sieves
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
• • 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
  • B01D2253/10—Inorganic adsorbents
  • B01D2253/106—Silica or silicates
  • B01D2253/11—Clays
• • 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
  • B01D2253/302—Dimensions
  • B01D2253/306—Surface area, e.g. BET-specific surface
• • 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
  • B01D2253/302—Dimensions
  • B01D2253/308—Pore size
• • 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
  • B01D2253/302—Dimensions
  • B01D2253/31—Pore size distribution
• • 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
  • B01D2253/302—Dimensions
  • B01D2253/311—Porosity, e.g. pore volume
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/50—Carbon oxides
  • B01D2257/504—Carbon dioxide
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2258/00—Sources of waste gases
  • B01D2258/02—Other waste gases
  • B01D2258/025—Other waste gases from metallurgy plants
• • 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 decarbonation, that is to say the separation of carbon dioxide (C0 2 ), a gas stream comprising said carbon dioxide, such as in gaseous flows of steel mills where Gaseous flows of carbon monoxide very often contain very large amounts of carbon dioxide.
• C0 2 present in more or less significant proportions, for example ranging from 15% to 60% by volume, in gas streams, including those containing a high content of carbon monoxide (at least 10%) and possibly hydrogen sulphide (10 ppmv to 5000 ppmv).
• gaseous flows to be decarbonized of steelworks which typically contain from 20% to 50% C0 2 and 20% to 50% CO, and that possibly minority species such as H 2 , N 2 , CH 4 , H 2 S, H 2 O.
• iron oxides are brought into contact with a reducing gas, which is often a mixture consisting essentially of CO and H 2 .
• This reducing gas reacts with the iron oxides forming elemental iron, CO 2 and H 2 0.
• the gas produced is therefore a mixture of CO 2 , H 2 O, CO and H 2 .
• this gas must be enriched again with CO and H 2 .
• One of the solutions may be the elimination of undesirable components, in particular the removal of impurities C0 2 and H 2 0, by separation, selective adsorption for example.
• US Pat. No. 8,192,524 describes a process for decarbonating a gas stream having a volume ratio of CO 2 greater than 10%, said method implementing at least one membrane unit comprising a plurality of polymer membranes in order to produce a permeate comprising at least 95% by volume of C0 2 and a gas stream depleted in C0 2 .
• at least one membrane unit comprising a plurality of polymer membranes in order to produce a permeate comprising at least 95% by volume of C0 2 and a gas stream depleted in C0 2 .
• US Pat. No. 4,459,142 discloses a cryogenic distillation process for the separation of C0 2 present in C 3 -C 10 hydrocarbon streams.
• processes using such cryogenic distillation systems have the disadvantage of having to manage the formation of dry ice at very low temperatures.
• the US5531808 patent describes the decarbonation of gas stream mainly comprising less polar gases than CO 2 , by passing said gas stream through a zeolite adsorbent X type of atomic Si / Al atom less than about 1, 15, at temperatures above 20 ° G
• US Pat. No. 7,608,134 proposes the use of a type X zeolite having an Si / Al atomic ratio of between 1.0 and 1.15, strongly exchanged with sodium, and agglomerated with a maximum binder content of 20%. to decarbonate gaseous flows, in particular air, polluted with C0 2 .
• US6143057 discloses composite adsorbents composed of zeolites in the form of microparticles smaller than 0.6 microns and a macroporous inert binder. These composite adsorbents are used to separate gaseous components present in gas mixtures, and in particular to separate the nitrogen or C0 2 present in the air.
• US Patent No. 6537348 B1 discloses the use of 0.5-3.0 mm NaLSX or LiLSX beads to decarbonate a gas having 50 mm Hg (67 mbar) of CO 2 .
• US Pat. No. 7,309,378 describes a process for purifying synthesis gases of the H 2 / CO OR H 2 / N 2 type , consisting in eliminating CO 2 as well as other impurities, by using an adsorbent of the NaLSX type and then by desorbent during a regeneration step that can be conducted by temperature rise (TSA) and / or pressure reduction (VSA, for "Volume Swing Adsorption” or PSA).
• TSA temperature rise
• VSA pressure reduction
• US Patent No. 6027545 discloses a method of producing iron directly reduced by using a gas composed of CO and H 2 (with impurities C0 2 , H 2 0 and CH 4 ) with a PSA unit which adsorbs C0 2 (and a little CO) to produce high purity H 2 , but without specifying the solids used.
• an objective of the present invention is the provision of a method for the decarbonation of gas flow containing a large amount of C0 2 , typically more than 15% of C0 2 , by volume relative to the total volume of flow. gaseous to decarbonate.
• Another object of the invention is to provide a decarbonation process of a gas stream leading to a final CO 2 content of less than 5%, better still less than 3%, and more preferably a final CO 2 content of 1%. of a few ppm, by volume relative to the total volume of said gas stream.
• Another objective is to propose a decarbonation process of a gas stream containing a large amount of CO 2, typically between 15% and 60%, or even between 20% and 50%, for example between 25% and 40%. , in volume relative to the total volume of gas stream to decarbonate, said process leading to a final content of C0 2 less than 5%, better still less than 3%, and better still a final content of C0 2 of the order of a few ppm, by volume relative to the total volume of said gas stream.
• Another objective is to provide a decarbonation process of gas stream implementing efficient means, economic, and compatible with a profitable industrial operation, and in particular with reduced energy costs and improved selectivity.
• the present invention relates to a decarbonation process of a gas stream, said process comprising at least the steps of: a) providing a gas stream containing from 15% to 60% of carbon dioxide, expressed as a volume in relation to the total volume of gas flow,
• the zeolite agglomerate comprises at least one binder and at least one zeolite and has a mesopore volume of 0.02 cm 3 .g -1 and 0.15 cm 3 .g -1 and a mesoporous volume fraction between 0 , 1 and 0.5, preferably between 0.15 and 0.45.
• the zeolite adsorbent in the form of agglomerates of the invention comprises both macropores, mesopores and micropores.
• Macropores means pores whose opening is greater than 50 nm.
• mesopores is meant pores whose opening is between 2 nm and 50 nm, limits not included.
• Micropores means pores whose opening is less than 2 nm, typically greater than strictly 0 and less than or equal to 2 nm.
• V ma the macroporous volume expressed in cm 3 .g _1 adsorbent
• V me the mesoporous volume expressed in cm 3 .g _1 adsorbent
• V mi the microporous volume expressed in cm 3 .g -1 of adsorbent.
• Macroporous volumes l / ma and mesoporous l / me are measured by porosimetry by intrusion of mercury.
• Such a mercury porosimeter Autopore 9500 Micromeritics ® is used to analyze the distribution of the pore volume contained in macropores and the mesopores.
• the experimental method described in the operating manual of the apparatus referring to ASTM D4284-83, consists of placing a sample of adsorbent (zeolite adsorbent in the form of agglomerates to be measured) (loss on ignition).
• adsorbent zeolite adsorbent in the form of agglomerates to be measured
• the relationship between the applied pressure and the characteristic dimension of the pore entry threshold (corresponding to an apparent pore diameter) is established using the Laplace-Young equation and assuming a cylindrical pore opening, a contact angle between mercury and pore wall of 140 ° and a mercury surface tension of 485 dynes / cm.
• the volume increments AVi of mercury introduced at each pressure level Pi are recorded, which then makes it possible to trace the accumulated volume of mercury introduced as a function of the applied pressure 1 / (Pi), or as a function of the apparent diameter of the pores V (li).
• the macroporous volume V ma of the adsorbent is defined as the cumulative volume of mercury introduced at a pressure of between 0.2 MPa and 30 MPa, corresponding to the volume contained in the pores with an apparent diameter greater than 50 nm.
• the mesoporous volume V me of the adsorbent is defined as the cumulative volume of mercury introduced at a pressure of between 30 MPa and 400 MPa.
• the method for measuring the pore volume by mercury intrusion does not allow access to the microporous volume, the total pore volume V tot as measured by mercury intrusion, corresponds to the sum of macroporous volumes V ma and mesoporous V me .
• the macroporous and mesoporous volumes V ma and V me as well as their sum (total pore volume V tot ), zeolite adsorbents, expressed in cm 3 .g -1 , are thus measured by intrusion porosimetry. of mercury and relative to the mass of the sample in anhydrous equivalent, that is to say the mass of said adsorbent corrected for loss on ignition.
• the term "decarbonation” is intended to mean the process for removing a gas stream containing CO 2
• “removal” means that the gas stream at the end of the process no longer contains C0 2 , or contains a quantity of C0 2 , less than 5%, better still less than 3%, and better still a final content of C0 2 of the order of a few ppm, in volume relative to the total volume said gas flow.
• the "C0 2 depleted" gas stream is called the gaseous flow at the end of the process, as described above.
• the process of the present invention is particularly suitable for the decarbonation of a gaseous flow containing from 15% to 60% of carbon dioxide (C0 2 ), preferably from 20% to 50%, more preferably from 25% to 50% by weight. % to 40% by volume relative to the total volume of said gas stream.
• C0 2 carbon dioxide
• the gas stream depleted in CO 2 comprises a quantity of CO 2 generally between a few ppmv and 10%, preferably from 0.01% to 5%, typically from 2 to 4%, but higher or lower values may be obtained depending on the intended applications.
• the method of the present invention is also particularly suitable for the decarbonation of gaseous flow comprising hydrogen sulfide (H2S), for example in concentrations between 10 ppmv to 5000 ppmv.
• H2S hydrogen sulfide
• Such gaseous flows with high C0 2 contents are present in a very large number of industrial fields, and in particular can be found in biogas, which can contain, for example, up to 50% C0 2 in the gases.
• biogas which can contain, for example, up to 50% C0 2 in the gases.
• said gas stream may contain CO contents of, for example, between 10% and 50%, in volume relative to the total volume of said gas stream, in natural gas which can contain up to 50% of C0 2 , but also the synthesis gas, such as for example those from the gasification of coal and which contain about 20 % C0 2 and about 20% to 50% CO, to name only the gas streams with high levels of C0 2 most common.
• gas streams that are most suitable for the process of the present invention are gas streams containing a content of CO 2 ranging from 15% to 60%, preferably from 20% to 50%, more preferably from 25% to 40%, more preferably about 35% by volume relative to the total volume of the gas stream.
• These particularly suitable gaseous flows furthermore contain, and preferably, one or more of the following gases:
• CO carbon monoxide
• H 2 hydrogen
• H 2 hydrogen
• methane (CH 4 ) generally from 0.5% to 50% by volume relative to the total volume of said gas stream, preferably from 1% to 20%, more preferably from 1% to 10%, typically about 1% % to 2%,
• H 2 0 water (H 2 0), generally from a few ppm (by volume, or ppmv) to 4%, typically about 3%,
• H 2 S hydrogen sulphide
• the zeolite agglomerate useful for the process of the present invention typically comprises zeolite crystals (s) agglomerated with a binder, which is preferably a clay binder.
• a binder which is preferably a clay binder.
• the amount of clay binder is generally between 1% and 30% by weight, preferably between 5% and 20% by weight, relative to the total weight of the zeolite adsorbent.
• the clay binder of the zeolite agglomerate useful for the process of the invention preferably comprises at least one clay selected from magnesium clays, and typically magnesium clay and a fibrous magnesium clay.
• fibrous magnesian clays is meant fibrous clays containing magnesium and preferably the hormones, the main representatives of which are sepiolite and attapulgite (or palygorskite). Sepiolite and attapulgite are the preferred hormones in the context of the present invention.
• a zeolitic adsorbent material whose binder comprises only one or more clays of the family of hormones.
• the binder comprises a mixture of clay (s) consisting of at least one fibrous magnesian clay, for example a hormite, and at least one other clay, for example chosen from montmorillonites, for example bentonite.
• binders comprising at least 50% by weight of at least one hormone relative to the total weight of the binder are preferred.
• the preferred clay mixtures are the mixtures sepiolite / bentonite and attapulgite / bentonite, more preferably attapulgite / bentonite, and very preferably those mixtures in which the hormones (sepiolite or attapulgite) are present at least 50% by weight. weight relative to the total weight of the binder.
• Said at least one zeolite of the zeolite agglomerate defined above is a zeolite in the form of crystals and preferably zeolite crystals of Faujasite type, for example zeolite crystals chosen from zeolites X, LSX, MSX, Y and mixtures thereof.
• Said zeolite crystals are preferably present in sodium form, and generally a sodium content, expressed as sodium oxide (Na 2 0) greater than 9.0% by weight of oxide relative to the total mass of the agglomerate.
• the zeolites described above all have an Si / Al atomic ratio of between 1 and 3 inclusive.
• the crystal content of zeolite (s) is generally between 70% and 99% by weight, preferably between 80% and 95% by weight relative to the total weight of the adsorbent.
• the zeolite agglomerate defined above may further comprise one or more additives and / or fillers well known to those skilled in the art, such as, for example, a porogenic agent, carboxymethylcellulose (CMC), an agent of reinforcement in general, fibers (such as fiberglass, carbon, Kevlar ® and others), carbon nanotubes (CNTs), colloidal silica, polymer, and other tissues.
• CMC carboxymethylcellulose
• the additive (s) and / or filler (s) represent at most 10% by weight, preferably at most 5% by weight relative to the total weight of the zeolitic adsorbent material that can be used in the context of the present invention.
• the zeolite adsorbent useful for the decarbonation process of the present invention has a very particular porous profile, characterized by:
• zeolite agglomerate used in the process of the present invention may be of any form known to those skilled in the art and for example in the form of yarns, beads, trilobed, for example and not limited to. However, it is preferred to use an adsorbent in the form of beads, and particularly beads having a particle size of between 0.5 mm and 5 mm, preferably between 1 mm and 3 mm, and more preferably between 1.6 mm and 2.5 mm. mm.
• agglomerated and shaped zeolite adsorbent materials made according to any techniques known to those skilled in the art are preferred, such as extrusion, compacting, agglomeration on a granulating plate, granulating drum, atomization and the like.
• This adsorbent zeolite agglomerate may be obtained according to techniques well known to those skilled in the art, and in particular by agglomeration of zeolite crystals with one or more clay (s) and optionally additives and other auxiliary agglomeration and formatting.
• the specific porous profile of the zeolite agglomerate used in the process of the invention can also be obtained according to standard techniques and well known to those skilled in the art, and for example by introducing one or more porogenic agent (s) (s). ) capable of creating mesoporosity by burning during the calcination of the zeolite agglomerate.
• the zeolite agglomerate described above may be used alone or in combination or mixed with one or more other zeolite (s) and / or other adsorbents.
• the zeolite agglomerate described above can be used in one or more superposed, alternating or sequenced beds.
• the process of the present invention allows the removal of large amounts of CO 2 , in particular large amounts of CO 2 present in a stream rich in CO, by means of an agglomerated zeolite adsorbent as defined hereinbelow. above.
• the characteristics of said zeolitic adsorbent confer in particular a high affinity for C0 2 and rapid adsorption kinetics.
• the process of the invention uses conventional and well-known adsorption techniques, and in particular adsorption techniques modulated by volume, pressure, temperature, volume and pressure. or in pressure and temperature.
• adsorption techniques modulated by volume, pressure, temperature, volume and pressure. or in pressure and temperature.
• These techniques are best known by their English acronyms VSA, PSA, TSA, VPSA and PTSA, respectively. It is particularly preferred to use the method according to the VSA, VPSA, PSA or PTSA technique, and more preferably according to the technical V SA, PSA or VPSA, especially for the decarbonation of gases rich in C0 2 and CO, such as steelworks gases.
• the method of the present invention can be implemented under the conditions of temperature and pressure well known to those skilled in the art.
• the process of the invention may be carried out at a temperature of between 0 ° C. and 100 ° C., preferably between 0 ° C. and 80 ° C., more preferably between 10 ° C. and 60 ° C., typically between 20 ° C and 50 ° C, panople at room temperature.
• the pressure applied throughout the process of the present invention may also vary in large proportions. However, it is preferred to operate with a pressure generally of between 200 kPa and 400 kPa, more preferably at a pressure of about 300 kPa.
• the process of the invention can be carried out in any type of process reactor known to those skilled in the art, capable of withstanding the operating conditions defined above, especially in terms of temperature and pressure, to achieve adsorption / regeneration cycles, typically of the VSA, PSA, TSA, VPSA and PTSA type, and for example and without limitation, reactor, filled column or not, tubular reactor, and others.
• the process of the invention can be carried out in one or more of the reactors defined above, placed in series or in parallel, in any suitable configuration, vertical and / or horizontal.
• one or more column reactors can be provided in parallel for the adsorption phases and one or more column reactors in parallel for the regeneration phases.
• the invention also relates to the use, for the decarbonation of a gaseous flow, of a zeolite agglomerate as defined above, that is to say comprising at least one binder and at least one zeolite, and having a mesoporous volume of between 0.02 cm 3 .g -1 and 0.15 cm 3 .g -1 and a mesoporous volume fraction of between 0.1 and 0.5, preferably between 0.15 and 0.45, as previously defined.
• the zeolite agglomerate comprises a binder, which is preferably a clay binder in an amount generally of between 1% and 30% by weight, preferably between 5% and 20% by weight, relative to the total weight of the zeolitic adsorbent.
• this clay binder preferably comprises at least one clay selected from magnesium clays, and typically magnesium clay and a fibrous magnesium clay selected from sepiolite and attapulgite. (or palygorskite), optionally in admixture with at least one other clay, for example chosen from montmorillonites, in particular bentonite.
• the binder is a mixture of clay, it is preferred that the binder comprises at least 50% by weight of at least one hormone relative to the total weight of the binder.
• the preferred clay mixtures are the mixtures sepiolite / bentonite and attapulgite / bentonite, more preferably attapulgite / bentonite, and most preferably those mixtures in which the hormones (sepiolite or attapulgite) are present at least 50% by weight. weight relative to the total weight of the binder.
• the zeolite crystals (s) of the zeolite agglomerate are preferably zeolite crystals of Faujasite type, for example zeolite crystals selected from zeolites X, LSX, MSX, Y and mixtures thereof. Said zeolite crystals are preferably present in sodium form, and generally a sodium content, expressed as sodium oxide (Na 2 0) greater than 9.0% by weight of oxide relative to the total mass of the agglomerate.
• the zeolites described above all have an Si / Al atomic ratio of between 1 and 3 inclusive.
• the crystal content of zeolites is generally between 70% and 99% by weight, preferably between 80% and 95% by weight relative to the total weight of the adsorbent.
• the zeolite agglomerate defined above may further comprise one or more additives and / or fillers well known to those skilled in the art, such as, for example, a porogenic agent, carboxymethylcellulose (CMC), an agent for reinforcement in general, fibers (such as fiberglass, carbon, Kevlar ® and others), carbon nanotubes (CNTs), colloidal silica, polymer, and other tissues.
• CMC carboxymethylcellulose
• the additive (s) and / or filler (s) represent at most 10% by weight, preferably at most 5% by weight relative to the total weight of the zeolitic adsorbent material that can be used in the context of the present invention.
• the zeolite agglomerate used in the process of the present invention may be of any form known to those skilled in the art, as indicated above.
• the zeolite agglomerate described above may be used alone or in combination with or in combination with one or more other zeolite agglomerate (s) and / or other adsorbents.
• the zeolite agglomerate described above can be used in one or more superposed, alternating or sequenced beds.
• zeolite agglomerate defined above for the decarbonation of a gaseous flow, and especially a gaseous flow containing from 15% to 60% (Volume) of carbon dioxide (CO 2 ), preferably from 20% to 50%, more preferably from 25% to 40% relative to the total volume of gas stream to be treated, has many advantages.
• the zeolite adsorbent of the invention has a very high capacity and a very high selectivity, and this, in particular because of the specific porous profile described above.
• the zeolite adsorbent in the use claimed in the present invention, has a very interesting life, and in particular longer than most that observed with other decarbonation systems known to the world. prior art.
• the zeolite agglomerate used in the process of the invention allows the creation of decarbonation units much compact, in terms of size, and much more energy-efficient.
• the use according to the present invention also allows to observe relatively short adsorption times, compared to those known from the prior art, and for example adsorption times of the order of 5 sec. at 10 min, preferably from 5 sec to 4 min and typically from 10 to 60 seconds.
• Another very interesting advantage is the fact that it is possible thanks to the zeolite agglomerate of the present invention, to carry out the regeneration steps in less reduced vacuum conditions than those required with the other decarbonation systems described. in the prior art.
• the C0 2 concentrations of the gas stream at the end of the process can thus easily be close to 5%, or even 3%, by volume, and even only a few ppmv.
• the zeolite agglomerate used in the process of the present invention is also a very versatile product and can therefore be used for a very wide variety of applications, particularly in the field of liquid or gaseous hydrocarbons , such as, for example, operations in drying, decarbonation, desulphurization, or in the fields of industrial gases, for example decarbonation of air, nitrogen / oxygen separation, and others.)
• the elemental chemical analysis of the zeolite agglomerate that can be used in the process of the invention can be carried out according to various analytical techniques known to those skilled in the art. Among these techniques, mention may be made of the technique of chemical analysis by X-ray fluorescence as described in standard NF EN ISO 12677: 201 1 on a wavelength dispersive spectrometer (WDXRF), for example the Tiger S8 spectrometer. from the Bruker company.
• WDXRF wavelength dispersive spectrometer
• X-ray fluorescence is a non-destructive spectral technique exploiting the photoluminescence of atoms in the X-ray domain to establish the elemental composition of a sample.
• the excitation of the atoms which is most often and usually performed by an X-ray beam or by electron bombardment, generates specific radiation after the atom has returned to the ground state.
• a measurement uncertainty of less than 0.4% by weight is obtained conventionally after calibration for each oxide.
• the X-ray fluorescence spectrum has the advantage of depending very little on the chemical combination of the element, which offers a precise determination, both quantitative and qualitative. A measurement uncertainty of less than 0.4% by weight is obtained conventionally after calibration for each oxide Si0 2 and Al 2 O 3 , as well as Na 2 0.
• AAS atomic absorption spectrometry
• ICP-AES inductively coupled plasma atomic emission spectrometry
• the elementary chemical analyzes described above allow both to verify the Si / Al atomic ratio of the zeolite used in the zeolite agglomerate and the Si / Al atomic ratio of said agglomerate.
• the measurement uncertainty of the Si / Al atomic ratio is ⁇ 5%.
• the measurement of the Si / Al atomic ratio of the zeolite present in the zeolite agglomerate can also be measured by solid nuclear magnetic resonance spectroscopy (NMR) of the silicon.
• the zeolite content in the zeolitic adsorbent material is evaluated by X-ray diffraction analysis (XRD), according to methods known to man of the job. This identification can be carried out using a Bruker DRX device.
• XRD X-ray diffraction analysis
• the zeolitic adsorbent materials are ground then spread and smoothed on a sample holder by simple mechanical compression.
• the interpretation of the diffractogram obtained is performed with the EVA software with identification of zeolites using the ICDD database PDF-2, release 201 1.
• the amount of zeolite fractions, by weight, is measured by XRD analysis on the Bruker D5000 device, then the amount by weight of the zeolite fractions is evaluated by means of the TOPAS software from the company Bruker.
• Sample A A2AW ® silica gel from KD Corporation in the form of beads 2-5 mm in size.
• Sample B zeolite agglomerate whose mesoporous volume is equal to 0.065 cm 3 .g -1 , and the mesoporous volume fraction is equal to 0.31 comprising about 20% of attapulgite binder and about 80% of FAU type zeolite of Si ratio In the range of 1, 19, the zeolite agglomerate is in the form of beads having a particle size of 1.6-2.5 mm.
• Sample C zeolite agglomerate similar to sample B, but wherein the agglomeration binder is sepiolite.
• the charge in an adsorption column of a pilot plant is identical with each sample and is equal to 379 g.
• the column of the adsorption pilot has a diameter of 2.2 cm and a height of 2 m.
• the height of the load in the column varies for each sample depending on the density of each sample:
• the gaseous mixture which feeds the adsorption column has a volume composition of 35% CO, 35% CO 2 , 10% N 2 and 20% H 2 .
• the feed rate is set at 8 NL.min _1 and 16 NL.min -1 at a temperature of 40 ° C and a pressure of 300 kPa.
• the regeneration is carried out for 100 seconds by reducing the pressure to a vacuum level of 20 - 30 kPa, comprising a purge step of 50 seconds under vacuum. using a gas with a volume composition of approximately 62% CO, 2.7% CO 2 and the balance 100% N 2.
• the total adsorption capacity C0 2 of the sample A and the sample B are compared in order to study the difference between a silica gel and a zeolite agglomerate.
• the gaseous mixture which feeds the column is as described above.
• the feed rate is set at 8 NL.min _1 at a temperature of 40 ° C and a pressure of 300 kPa. As indicated previously, the same amount of 379 g adsorbent is used for each sample.
• the adsorption phase is stopped when the samples are completely saturated in C0 2 , that is to say that the concentrations of the constituents of the incoming gas stream are identical to those of the outgoing gas stream.
• the adsorption time required for each sample to obtain its total saturation is as follows:
• the piercing time to reach a volume concentration of 0.1% C0 2 , for each sample, is:
• sample B zeolite agglomerate according to the invention
• sample A sica gel, comparative sample
• sample B zeolite agglomerate according to the invention
• zeolite agglomerate according to the invention leads to a much longer period of use than when a silica gel is used, if the same amount of adsorbent is used or the adsorption unit can be made more compact by using a zeolite agglomerate rather than a silica gel, thereby reducing both investment and operating costs.
• this example compares the dynamic adsorption capacities of C0 2 samples A and C to study the differences between a silica gel and a molecular sieve.
• the feed rate is set at 16 NL.min _1 at a temperature of 40 ° C and a pressure of 300 kPa.
• the amount of each sample used is 379 g.
• the adsorption phase is stopped when the C0 2 volume concentration of the outgoing gas stream reaches 2.6% (piercing concentration).
• the regeneration is carried out for 100 seconds by reducing the pressure to a vacuum level of 20 kPa, comprising a purge step of 50 seconds under vacuum at the same time. using a gas of volume composition of about 62% CO, 2.7% C0 2 and the complement 100% N 2 . Fifteen (15) adsorption / desorption cycles are performed to achieve a stable pierce time for each sample.
• the piercing time to reach a volume concentration of 2.6% C0 2 , for each sample, is:
• the sample C (zeolite agglomerate according to the invention) has a performance of 2.5 times more than the sample A (silica gel, comparative sample) and so that using a zeolite agglomerate the duration of use will be longer than with a silica gel, if the same amount of adsorbent is used, due to the possibility of decreasing the number of regeneration cycles.
• this example compares the dynamic adsorption capacities of CO 2 of samples A and C in order to study the differences between a silica gel and a molecular sieve.
• the feed rate is set at 16 NL.min _1 , the temperature at 40 ° C and the pressure at 300 kPa.
• the amount of each sample used is 379 g.
• the regeneration of each of samples A and C is compared to study the differences between a silica gel and a zeolite agglomerate.
• the gaseous mixture entering the adsorption column has a volume composition of 35% CO, 35% C0 2 , 10% N 2 and 20% H 2 .
• the feed rate is set at 8 NL.min _1 , the temperature at 40 ° C and the pressure at 300 kPa.
• the amount of adsorbent is identical for each sample and is 379 g.
• the adsorption phase is stopped when the volume concentration of CO 2 reaches 2.6% (drilling concentration).
• the regeneration is carried out for 100 seconds by reducing the pressure to a certain specific vacuum level, comprising a purge step of 50 seconds under vacuum using a gas with a volume composition of approximately 62% CO, 2.7% C0 2 and 100% N 2 complement.
• the specific vacuum level mentioned above varies according to the sample in order to obtain the same drilling time of 36 seconds (stable after a multitude of cycles) in order to obtain an output volume concentration of 2.6% in C0 2 for each sample. Fifteen (15) adsorption / desorption cycles are performed to achieve a stable pierce time for each sample.
• the level of vacuum required for each sample is:
• sample C zeolite agglomerate according to the invention
• A sica gel, comparative sample
• sample C it is possible to reduce operational costs during regeneration.

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