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WO2024132899A1 - Utilisations de sorbants aminés pour la capture de co2 à partir de courants gazeux - Google Patents

Utilisations de sorbants aminés pour la capture de co2 à partir de courants gazeux Download PDF

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Publication number
WO2024132899A1
WO2024132899A1 PCT/EP2023/086001 EP2023086001W WO2024132899A1 WO 2024132899 A1 WO2024132899 A1 WO 2024132899A1 EP 2023086001 W EP2023086001 W EP 2023086001W WO 2024132899 A1 WO2024132899 A1 WO 2024132899A1
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carbon dioxide
exchange
sorbent material
particles
gas mixture
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Davide Albani
Cornelius GROPP
Tomas AZTIRIA
Claudio LIMONE
Angelo VARGAS
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Climeworks AG
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Climeworks AG
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    • 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
    • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
    • B01J20/28016—Particle form
    • 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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
    • B01J20/26—Synthetic macromolecular compounds
    • B01J20/265—Synthetic macromolecular compounds modified or post-treated polymers
    • B01J20/267—Cross-linked polymers
    • 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
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
    • 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
    • B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • B01J41/04—Processes using organic exchangers
    • 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
    • B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • B01J41/04—Processes using organic exchangers
    • B01J41/05—Processes using organic exchangers in the strongly basic form
    • 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
    • B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • B01J41/08—Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • C22B11/042—Recovery of noble metals from waste materials
    • C22B11/048—Recovery of noble metals from waste materials from spent catalysts
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B61/00—Obtaining metals not elsewhere provided for in this subclass
    • 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
    • B01D2253/20—Organic adsorbents
    • 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
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/02—Non-contaminated water, e.g. for industrial water supply
    • C02F2103/04—Non-contaminated water, e.g. for industrial water supply for obtaining ultra-pure water

Definitions

  • the present invention relates to sorbent materials as used for capturing carbon dioxide from gas streams as well as to uses thereof, in particular downcycling applications of materials which have been used as sorbent materials for capturing carbon dioxide from air, in particular atmospheric air in direct air capture processes.
  • Flue gas capture or the capture of CO2 from point sources, such as specific industrial processes and specific CO2 emitters, deals with a wide range of relatively high concentrations of CO2 (3-100 vol %) depending on the process that produces the flue gas.
  • High concentrations make the separation of the CO2 from other gases thermodynamically more favorable and consequently economically favorable as compared to the separation of CO2 from sources with lower concentrations, such as ambient air, where the concentration is in the order of 400 ppmv.
  • the very concept of capturing CO2 from point sources has strong limitations: it is specifically suitable to target such point sources, but is inherently linked to specific locations where the point sources are located and can at best limit emissions and support reaching carbon neutrality, while as a technical solution it will not be able to contribute to negative emissions (i.e., permanent removal of carbon dioxide from the atmosphere) and to remove emission from the past.
  • negative emissions i.e., permanent removal of carbon dioxide from the atmosphere
  • the two most notable solutions currently applied are the capturing of CO2 by means of vegetation (i.e., trees and plants, but not really permanent removal) using natural photosynthesis, and by means of DAC technologies, which is the only really permanent removal.
  • DAC technologies were described, such as for example, the utilization of alkaline earth oxides to form calcium carbonate as described in US-A-2010034724.
  • Different approaches comprise the utilization of solid CO2 adsorbents, hereafter named sorbents, in the form of packed beds of typically sorbent particles and where CO2 is captured at the gas-solid interface.
  • Such sorbents can contain different types of amino functionalization and polymers, such as immobilized aminosilane-based sorbents as reported in US-B-8,834,822, and amine-functionalized cellulose as disclosed in WO-A-2012/168346.
  • WO-A-2011/049759 describes the utilization of an ion exchange material comprising an aminoalkylated bead polymer for the removal of carbon dioxide from industrial applications.
  • WO-A-2016/037668 describes a sorbent for reversibly adsorbing CO2 from a gas mixture, where the sorbent is composed of a polymeric adsorbent having a primary amino functionality. The materials can be regenerated by applying pressure or humidity swing.
  • the state-of-the-art technology to capture CO2 from point sources typically uses liquid amines, as for example in industrial scrubbers, where the flue gas flows into a solution of an amine (US-B-9, 186,617).
  • Other technologies are based on the use of solid sorbents in either a pack-bed or a flow-through structure configuration, where the sorbent is made of impregnated or covalently bound amines onto a support.
  • Amines react with CO2 to form of a carbamate moiety, which in a successive step can be regenerated to the original amine, for example by increasing the temperature of the sorbent bed to ca 100°C and therefore releasing the CO2.
  • An economically viable process for carbon capture implies the ability to perform the cyclic adsorption/desorption of CO2 for hundreds or thousands of cycles over the same sorbent material, where the sorbent shall not undergo significant chemical transformations that impedes its reactivity towards CO2. Shi et al. (Sorbents for the Direct Capture of CO2 from Ambient Air, Angew. Chem. Int. Ed.
  • WO-A-9822173 relates to a regenerative absorber device for the removal of CO2 from expiration gases during anesthesia.
  • the device comprises a container having an inlet for said expiration gases, and an outlet for output gases, the CO2 content of which having been substantially removed therefrom.
  • the device is provided with an ion exchanger having the capability to absorb CO2, disposed in said container such that the gases flow through said ion exchanger from said inlet to said outlet.
  • a novel method of anesthesia comprises use of a CO2 absorber device according to the invention.
  • GB-A-1296889 reports how carbon dioxide is separated from mixtures with non-acid gases such as air by sorption on a weakly basin ion exchange resin followed by desorption with steam under conditions such that the steam condenses at the inlet end of the resin bed and a front of condensing steam then progressively passes through the bed displacing the carbon dioxide. Sorption is suitably conducted at 40-90 F and at a relative humidity of 75- 90%.
  • the preferred ion exchanger is a polystyrene-divinylbenzene copolymer containing polyamino functional groups, each of which comprises at least one secondary amino nitrogen atom.
  • Lewatit VP OC 1065 is proposed as ion exchange material as immobilised primary or secondary amine groups on solid supports, a material known for use in the selective removal of acids from process streams, the decolorization of sugar starch and protein solutions, the adsorption of aldehydes and other chemicals.
  • EP-A-2490789 proposes a process for the reduction of carbon dioxide (or CO2) from various types of gas emitting sources containing carbon dioxide, including the reduction of carbon dioxide from industrial gas emitting sources via the use of an ion exchange material.
  • WO-A-2022/128431 proposes a method for separating gaseous carbon dioxide from air by cyclic adsorption/desorption using a sorbent, wherein the method comprises the following sequential and in this sequence repeating steps: (a) contacting air with the sorbent to allow gaseous carbon dioxide to adsorb on the sorbent under ambient atmospheric pressure and temperature conditions; (b) isolating said sorbent from said flow-through; (c) inducing an increase of the temperature of the sorbent; (d) extracting the desorbed gaseous carbon dioxide from the unit and separating gaseous carbon dioxide from steam/water; (e) bringing the sorbent to ambient atmospheric temperature and pressure conditions.
  • Said sorbent is a water retaining and/or porous support which before use in the cyclic process has been impregnated or wetted with a solution of a secondary amine compound and said sorbent is loaded by said secondary amine compound by at least 5% by weight.
  • Amines react with CO2 to form of a carbamate moiety, which in a successive step can be regenerated to the original amine, for example by increasing the temperature of the sorbent bed to ca 100°C and therefore releasing the 002.
  • An economically viable process for carbon capture implies the ability to perform the cyclic adsorption/desorption of 002 for hundreds or thousands of cycles over the same sorbent material, where the sorbent shall not undergo any or if at all only insignificant chemical transformations that impedes its reactivity towards 002.
  • Adsorption and desorption cycles of 002 capture from a gas stream occur in the presence of varying amount of oxygen, and in particular desorption cycles involve a temperature swing, where the sorbent bed is heated to a temperature in the range of 100°C. Under such conditions amines can react with oxygen to form adducts. Examples of such adducts of linear secondary amines are depicted below:
  • benzylamine moieties are the following:
  • Oxidative degradation of primary and secondary amine-based solid sorbents is thought to involve hydrogen abstraction from the a-carbon to the amine functionality and to the formation of e.g. an amide.
  • the major products of amine oxidative degradation are exemplified above.
  • the position of attack of the oxygen occurs at the a-carbon to the amine functionality, resulting in the loss of ability of the nitrogen atom to bind CO2 and required the a-carbon to be substituted with at least one hydrogen.
  • the materials which can be used in carbon dioxide capture processes can also be used in different fields of technology as exchange materials.
  • DAC direct air capture
  • IER materials flue gas capture
  • These uses involve large amounts of corresponding material and in these uses normally degradation is no or only a much smaller problem, and if degradation is, it involves different degradation paths, like fouling and loss of particles and the like.
  • Sorbents with different degree of oxidation and hence different CO2 capacities were titrated using a standard method (exchange capacity) used for qualifying IER in water treatment.
  • Sorbents that have reached end of life for DAC are therefore highly interesting materials for water treatment (IER) and other exchange applications different from carbon dioxide capture.
  • IER water treatment
  • the gist of the present invention is therefore that after having reached a point where ion exchange resin materials are not good enough for the economy of the DAC process, these materials can still very economically and ecologically be used as exchange material in different processes, for example as ion exchanger.
  • a first aspect of the present invention relates to the use of an ion exchange material which before has been used as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process in a secondary exchange process, different from said reversible separation of carbon dioxide from a gas mixture, with at least partial immersion in a liquid.
  • the secondary exchange process is correspondingly a process in which the ion exchange material is at least partially immersed in a liquid.
  • the secondary exchange process is a process where the exchange takes place between the ion exchange material and the liquid, or substances dissolved/suspended/dispersed in that liquid, in the region of immersion.
  • the secondary exchange process for example can be a typical ion exchange process, where ions which are dissolved and hydrated in the liquid are absorbed on the ion exchange material.
  • the invention relates to the concept of using a material, which has been used as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process, and which has been degraded in that process due to intensive use, in the context of a secondary exchange process which is different from said carbon dioxide capture process.
  • a secondary exchange process which is different from said carbon dioxide capture process.
  • it relates to the use of an ion exchange material in a secondary exchange process with at least partial immersion in a liquid, preferably complete immersion of the ion exchange material in a liquid, preferably water.
  • the ion exchange material which is used in the secondary exchange process is a material which had acted as absorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process.
  • the ion exchange material which is used in the secondary exchange process thus has the properties being the result of having been modified in the process of reversible separation of carbon dioxide from a gas mixture in a cyclic process.
  • the ion exchange material is characterized by a corresponding modification of the adsorption properties due to that previous reversible separation of carbon dioxide exposure.
  • the invention relates to the use of an ion exchange material in an exchange process involving at least partial, preferably complete immersion of the ion exchange material in a liquid, preferably water, wherein the ion exchange material is a material modified by reversible separation of carbon dioxide from a gas mixture in a cyclic process.
  • partial immersion in the secondary exchange process in a liquid means that the ion exchange material, for the very purpose and for carrying out the secondary exchange process, is immersed in that liquid, and the exchange process takes place by way of exchange between the liquid and/or substances contained, dissolved or suspended or dispersed therein, and the ion exchange material.
  • the present invention relates to a method, in which in a first step and ion exchange material is used as adsorbent material and is subjected to a process of reversible separation of carbon dioxide from a gas mixture in a cyclic process.
  • this ion exchange material is then used in a secondary exchange process different from said reversible separation of carbon dioxide from a gas mixture, and that secondary exchange process involves at least partial immersion of the ion exchange material in a liquid, preferably complete immersion in the liquid, preferably the liquid is water or is primarily based on water.
  • the sorbent material due to the preceding use as sorbent material for the reversible separation of carbon dioxide from a gas mixture, the sorbent material, compared to an initial carbon dioxide capture capacity before first use in this process evaluated in mmol/g, has lost at least 20% of its carbon dioxide capture capacity, preferably at least 30% or at least 40% or at least 50%.
  • the carbon dioxide capture capacity before first use was in the range of 1.5-2 mmol/g or even 1.5 - 3 mmol/g in the pristine condition before having been used in the capture process, and due to the carbon dioxide capture process use it has degraded to have a carbon dioxide capture capacity value of less than 1.5 mmol/g, typically in the range of 0.2-1.4 mmol/g.
  • such a material still has an exchange capacity typically in the range of 4-7, preferably in the range of 4.5-6.75 mmol/g, so it is perfectly and very efficiently usable for the secondary exchange use, in particular for example for water treatment.
  • the preceding use as sorbent material for the reversible separation of carbon dioxide from a gas mixture has taken place over a time span of at least 5 days, preferably at least 10 days, or at least 20 days or at least one month or at least 3 or at least 6 months or at least one or at least 2 or at least 3 years.
  • Said use as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process has for example been in a method for separating gaseous carbon dioxide from a gas mixture, preferably from at least one of ambient atmospheric air, flue gas and biogas, preferably ambient atmospheric air, containing said gaseous carbon dioxide as well as further gases different from gaseous carbon dioxide, by cyclic adsorption/desorption using a sorbent material adsorbing said gaseous carbon dioxide in a unit, wherein the cyclic process comprises at least one of a thermal swing, a pressure swing or humidity swing, preferably a combination of at least two of such swings.
  • a sorbent material for separating gaseous carbon dioxide from a gas mixture preferably from at least one of ambient atmospheric air, flue gas and biogas, preferably for direct air capture
  • a temperature, vacuum, or temperature/vacuum swing process preferably using a process in which injecting a stream of partially of fully saturated or superheated steam by flow-through the unit is used for inducing an increase of the temperature of the sorbent material to a temperature between 60 and 110°C, resulting in the at least partial desorption of CO2.
  • the method for separating gaseous carbon dioxide from the gas mixture has preferably been a method, which comprises at least the following sequential and in this sequence repeating steps (a) - (e):
  • This is e.g. possible by injecting a stream of partially of fully saturated or superheated steam, preferably by flow- through through the unit and over/through the sorbent, and thereby inducing an increase of the temperature of the sorbent material to a temperature between 60 and 110°C, starting the desorption of CO2;
  • the ambient atmospheric temperature established in this step (e) is in the range of the surrounding ambient atmospheric temperature +25°C, preferably +10°C or +5°C).
  • ambient atmospheric pressure and “ambient atmospheric temperature” refer to the pressure and temperature conditions to that a plant that is operated outdoors is exposed to, i.e. typically ambient atmospheric pressure stands for pressures in the range of 0.8 to 1.1 barabs and typically ambient atmospheric temperature refers to temperatures in the range of -40 to 60° C, more typically -30 to 45°C.
  • the gas mixture used as input for the process is preferably ambient atmospheric air, i.e. air at ambient atmospheric pressure and at ambient atmospheric temperature, which normally implies a CO2 concentration in the range of 0.03-0.06% by volume, and a relative humidity in the range of 3-100%. However, also air with lower relative humidity, i.e.
  • ⁇ 3%, or with lower or higher CO2 concentration can be used as input for the process, e.g. with a concentration of 0.1 -0.5% CO2 by volume, so generally speaking, preferably the input CO2 concentration of the input gas mixture is in the range of 0.01-0.5% by volume.
  • the pressure in the unit (preferably at the end of this step) is in the range of 500-1000 mbarabs, preferably in the range of 550-1000 mbarabs or 600-950 mbarabs.
  • step (d) may include reduction of the pressure in the unit to values between 20- 500 mbarabs, preferably 50-250 mbarabs by means of evacuation, which causes evaporation of water from the sorbent subsequently both drying and cooling the sorbent.
  • the said sorbent material comprises or consists of a porous structure of particles of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide.
  • this is preferably having a thickness in the range of 0.1-4 mm, or in the range of 0.2-2 mm, and or having a thickness in the range of 0.4-1 .1 mm.
  • the monolith When taking the form of a monolith, the monolith preferably takes the form of a structure having, in the direction of gas flow in operation, a plurality of through openings of preferably polygonal or round cross-section, preferably triangular, rectangular or square, pentagonal or hexagonal, oval or circular cross-section, wherein preferably the monolith takes the form of a honeycomb structure.
  • such a contiguous three-dimensional structure has a length in adsorption flow direction in the range of 0.1-3 m.
  • the sorbent material preferably in the form of particles, is based on or consists of support material functionalized (on the surface and/or in the bulk) with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide, preferably in the form of ion exchange resin (I ER) particles, which can either be manufactured at the desired size or which can be ground before the carbon dioxide capture process to the desired size.
  • support material functionalized (on the surface and/or in the bulk) with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide, preferably in the form of ion exchange resin (I ER) particles, which can either be manufactured at the desired size or which can be ground before the carbon dioxide capture process to the desired size.
  • I ER ion exchange resin
  • the contiguous three-dimensional structure of the sorbent adsorbs gaseous carbon dioxide by at least one of flow over and flow-through, preferably by a combination of flow over and flow-through of the gas mixture in step (a).
  • the sorbent material preferably in the form of particles, comprises or consists of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide and which comprises or consists of organic cross linked polymeric polystyrene based support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, preferably cross-linked by divinylbenzene.
  • the polystyrene-based support material is a styrene divinylbenzene copolymer, preferably to form the sorbent material surface and/or in the bulk functionalised with primary amine, preferably methyl amine, most preferably benzylamine moieties, wherein the solid polymeric support material is preferably obtained in a suspension polymerisation process.
  • Step (c) typically involves injecting a stream of partially of fully saturated or superheated steam, preferably by flow-through through said unit for heating the sorbent.
  • the sorbent material preferably particles, of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide preferably have a nitrogen content in the range 4 - 50 wt.%, preferably in the range of 5 - 25 wt.% or 5 - 15 wt.% or 6 -12 wt.%, in each case for dry sorbent material.
  • the process is a direct air capture process, which means the gas mixture is ambient atmospheric air.
  • the secondary exchange process is selected from one or a combination of the group consisting of:
  • liquid metal purification or exchange process including metal catalyst recovery or exchange, metal enrichment, metal recycling recovery,
  • the liquid purification process or exchange process for example the water purification process, is typically an ion exchange process in which ions dissolved in the water are adsorbing on the ion exchange material and are therefore removed from the water into which the ion exchange material is immersed. Then in a second regeneration step the ion exchange system is separated from the liquid to be purified (for example by filtration) and subjected to a regenerant solution, in which the ion exchange material due to the different chemical nature of that regenerant solution, releases the adsorbed ions, such that the ions are enriched in and/or carried away by the regenerant solution and thus removed from the material, which can then be reused.
  • a regenerant solution in which the ion exchange material due to the different chemical nature of that regenerant solution, releases the adsorbed ions, such that the ions are enriched in and/or carried away by the regenerant solution and thus removed from the material, which can then be reused.
  • the regenerant solution can be water-based but having a different salt concentration and/or a different temperature and/or a different pH, or it can be a liquid different from the one to be purified. So if the liquid to be purified is water, the regenerant solution can be a mixture of water with another solvent or can be just that other solvent or a mixture of non-water solvents. Using a different solvent as regenerant can be combined with different saline concentrations, pH and temperature, for regeneration.
  • Said sorbent material preferably comprises or consists of a material, preferably in the form of particles, of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide.
  • the mean particle size (D50, by volume, e.g. measured using sieving methods) of such particles of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide is in the range of 0.001 - 4 mm, preferably 0.1 - 2 mm.
  • the use as a sorbent material for the reversible separation of carbon dioxide from a gas mixture is in the form of a packed bed particle adsorber, or in the form of a contiguous layer or monolithic structure, in both cases preferably based on particles, and wherein the secondary use is in the form of particles, in particular a packed bed of particles, or in the form of a contiguous layer or monolithic structure, preferably in both cases based on particles.
  • the particles can be disintegrated mechanically and/or chemically from the contiguous structure to particles before the secondary use.
  • Said sorbent material normally comprises or consists particles of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide, which particles comprise or consist of organic cross linked polymeric polystyrene based support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, preferably cross-linked by divinylbenzene, wherein further preferably the polystyrene based support material is a styrene divinylbenzene copolymer, preferably to form the sorbent material surface and/or in the bulk functionalised with primary amine, preferably methyl amine, most preferably benzylamine moieties, wherein the solid polymeric support material is preferably obtained in a suspension polymerisation process.
  • Said sorbent material further preferably comprises or consists particles of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide, which particles comprise or consist of organic cross linked polymeric polystyrene based support material in the form of a styrene divinylbenzene copolymer, to form the sorbent material surface and/or in the bulk functionalised with primary amine, preferably methyl amine, most preferably benzylamine moieties.
  • said sorbent material is a benzyl amine-co- polystyrene based ion exchange resin, preferably produced by a phthalimide addition or a chloromethylation process.
  • the sorbent material When defining the sorbent material this is defining its condition in the carbon dioxide capture process.
  • the sorbent material can be used in the same condition, however it can also be modified for that secondary exchange process, in particular and preferably by chemical modification of the primary and/or secondary amine functionality of the sorbent material.
  • said sorbent material after its use as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process comprises or consists of a material, preferably in the form or particles, of support material functionalized on the surface and/or in the bulk with primary or secondary amines, or a combination thereof, capable of reversibly binding carbon dioxide, and before its use in a secondary exchange process different from said reversible separation of carbon dioxide from a gas mixture the material is modified at the primary and/or secondary amines for the secondary exchange process.
  • this modification takes the form of a quaternization, preferably to convert into a strong base ion exchange resin, or the form of a methylphosphonation, preferably to convert into a chelating ion exchange resin.
  • the present invention relates to a method for operating an exchange process selected from the group consisting of: liquid purification or exchange process, including water purification, silica removal, industrial demineralisation, steam purification, chemical purification or exchange, including purification or exchange of organic molecules such as aldehydes, purification or exchange of biological molecules including proteins, peptides, antibodies and derivatives thereof; liquid metal purification or exchange process, including metal catalyst recovery or exchange, metal enrichment, metal recycling recovery, condensate polishing.
  • liquid purification or exchange process including water purification, silica removal, industrial demineralisation, steam purification, chemical purification or exchange, including purification or exchange of organic molecules such as aldehydes, purification or exchange of biological molecules including proteins, peptides, antibodies and derivatives thereof
  • liquid metal purification or exchange process including metal catalyst recovery or exchange, metal enrichment, metal recycling recovery, condensate polishing.
  • This method is characterised in that this exchange process (which is the secondary exchange process as detailed further above) is carried out with an ion exchange material which before has been used as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process.
  • This reversible cyclic separation of carbon dioxide from a gas mixture can be as specified further above, preferably it is a direct air capture process.
  • the present invention relates to an ion exchange material which before has been used as sorbent material for the reversible separation of carbon dioxide from a gas mixture in a cyclic process for use in in a secondary exchange process different from said reversible separation of carbon dioxide from a gas mixture with at least partial immersion in a liquid. Further embodiments of the invention are laid down in the dependent claims.
  • Fig. 1 shows on the x-axis the exchange capacity in mmol/g and on the Y axis the carbon dioxide capture capacity in mmol/g for six experimentally determined systems.
  • the sorbent beads employed are based on porous divinyl benzene crosslinked polystyrene beads (d ⁇ 0.3-1.5 mm) functionalized with amino methyl-groups to form benzyl amine moieties which can be introduced e.g. in an chloromethylation reaction followed by amination with urotropine.
  • the sorbent beads used can by synthesized as follows: In a 1 L reactor, 1 % (mass ratio) of gelatin and 2% (mass ratio) of sodium chloride are dissolved in 340 mL of water at 45°C for 1 h. In another flask, 1 g of benzoyl peroxide is dissolved in a mixture of 59.7 g of styrene, 3.9 g of divinylbenzene (content 80%) and 65.3 g of C11-C13 iso-paraffin. The resulting mixture is then added to the reactor.
  • reaction mixture is stirred and heated up to 70°C maintaining the temperature for 2 h, then the temperature is raised to 80°C and kept it for 3 h, and then raised to 90°C for 6 h.
  • the reaction mixture is cooled down to room temperature and the beads are filtered off using a funnel glass filter and vacuum suction. The beads are washed with toluene and dried in rotavapor.
  • the polystyrene-divinylbenzene beads are functionalized using the chloromethylation reaction. 5 g of so obtained beads are added to a 3-neck flask containing 50 mL of chloromethyl methyl ether. The mixture is stirred for 1 h, 2 g of zinc chloride is added and is heated to 40°C and kept it for 24 h. After that, the beads are filtered off and washed with 25% HCI and water to obtain chloromethylated beads. To obtain benzylamine units, the chloromethylated beads are aminated using the following procedure. The chloromethylated beads are added to a three-necked flask with 27 g of methylal and the mixture is stirred for 1 h.
  • the amine is protonated and to free the base, the beads are treated with 50 mL of an NaOH solution 2 M, and stirred with 1 h at 80°C. The aminated beads are filtered off and washed to neutral pH with demineralized water.
  • the synthesis route can be illustrated as follows:
  • Samples were either degraded in an oven under air flow for multiple days of exposure or were taken from life test experiments where the sorbent was cycled for thousands of cycles under a temperature vacuum swing process.
  • the sorbent that was degraded in the oven was treated in the following way: 60 g of sorbent (solid content 75 wt.%) were placed in a stainless steel reactor and continuously exposed to a mixture of synthetic air O2/N2 at a temperature of 90 °C for a period of 3 and 18 days.
  • the sorbent that was degraded during the life test was treated in the following way: 200 g of sorbent (solid content 75 wt.%) were placed in a stainless steel reactor and subjected to a cyclic adsorption and desorption process.
  • the desorption process consisted in pulling the vacuum at room temperature and then heat up to ca 100°C by injecting steam to the reactor chamber.
  • the sorbent was cycled for many thousand cycles and samples were taken at different intervals.
  • 6 g of dry sample was filled into a cylinder with an inner diameter of 40 mm and a height of 40 mm and placed into a CO2 adsorption/desorption device, where it was exposed to a flow of 2.0 NL/min of air at 30°C containing 450 ppmv CO2, having a relative humidity of 60% corresponding to a temperature of 30°C for a duration of 600 min.
  • the sorbent bed Prior to adsorption, the sorbent bed was desorbed by heating the sorbent to 94°C under an air flow of 2.0 NL/min.
  • the amount of CO2 adsorbed on the sorbent was determined by integration of the signal of an infrared sensor measuring the CO2 content of the air stream leaving the reactor.
  • Solid content is measured with a Halogen Moisture Analyzer (Adam Equipment PMB Moisture Analyzer); measurement temperature is 110°C, the measurement stops automatically at constant weight (0.002g/15s).
  • Halogen Moisture Analyzer Adam Equipment PMB Moisture Analyzer
  • the used sorbent material prior to any use in a carbon dioxide capture process exhibits a carbon dioxide capture capacity in the range of 2.0 mmol/g, and in exchange capacity of about 7.2 mmol/g (data illustrated on top right).
  • the carbon dioxide capture capacity of the ion exchange resin particles reduces to values in the range of 1.25 mmol/g, so there is a reduction of almost 40% in the carbon dioxide capture capacity.
  • the exchange capacity is only reduced to values in the range of 6-6.5 mmol/g, so the reduction is only in the range of 15%.
  • the degradation relevant for the carbon dioxide capture process seems to be only little correlated with the degradation relevant for the exchange process.
  • Sorbents after end of operation in DAC therefore can be reused in other exchange processes, so for example in the water treatment industry, which presents highly sustainable downcycling (analogy with the battery materials industry).

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Abstract

La présente invention concerne l'utilisation d'un matériau échangeur d'ions qui auparavant a été utilisé comme matériau sorbant pour la séparation réversible du dioxyde de carbone à partir d'un mélange gazeux dans un procédé cyclique dans un processus d'échange secondaire, différent de ladite séparation réversible de dioxyde de carbone à partir d'un mélange gazeux, avec une immersion au moins partielle dans un liquide.
PCT/EP2023/086001 2022-12-21 2023-12-15 Utilisations de sorbants aminés pour la capture de co2 à partir de courants gazeux Ceased WO2024132899A1 (fr)

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