US20150139887A1 - Materials and process for reversible adsorption of carbon dioxide - Google Patents

Materials and process for reversible adsorption of carbon dioxide Download PDF

Info

Publication number
US20150139887A1
US20150139887A1 US14/415,147 US201314415147A US2015139887A1 US 20150139887 A1 US20150139887 A1 US 20150139887A1 US 201314415147 A US201314415147 A US 201314415147A US 2015139887 A1 US2015139887 A1 US 2015139887A1
Authority
US
United States
Prior art keywords
carbon dioxide
solid material
water
temperature
less
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.)
Abandoned
Application number
US14/415,147
Other languages
English (en)
Inventor
Timo Roestenberg
Gerrit Brem
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Antecy BV
Original Assignee
Antecy BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Antecy BV filed Critical Antecy BV
Priority to US14/415,147 priority Critical patent/US20150139887A1/en
Priority claimed from PCT/EP2013/065070 external-priority patent/WO2014012963A1/fr
Publication of US20150139887A1 publication Critical patent/US20150139887A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • 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
    • 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
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/261—Drying gases or vapours by adsorption
    • 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
    • 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
    • B01J20/28042—Shaped bodies; Monolithic structures
    • B01J20/28045—Honeycomb or cellular structures; Solid foams or sponges
    • C01B31/20—
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/306—Alkali metal compounds of potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • 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
    • B01D2253/102—Carbon
    • 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
    • B01D2253/25—Coated, impregnated or composite 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
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40056—Gases other than recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention relates generally to the reversible adsorption of carbon dioxide from a gas mixture, and more particularly to the reversible adsorption of carbon dioxide from ambient air.
  • Carbon dioxide has been identified as a major contributor to climate change. Significant efforts are being made towards the development of adsorbent materials that adsorb carbon dioxide from gas mixtures, such as flue gases, that are relatively carbon dioxide rich. The focus is on adsorbent materials that irreversibly capture the carbon dioxide, for example calcium oxide. By sequestering the captured carbon dioxide in, for example, landfills or abandoned mines in the form of calcium carbonate, the amount of carbon dioxide in the atmosphere is effectively reduced.
  • carbon dioxide capture is considered reversible if the release of captured carbon dioxide can be accomplished at temperatures below 300° C. For economic reasons it is desirable for the desorption of carbon dioxide to take place at even lower temperatures, for example less than 200° C.
  • ambient air has a low carbon dioxide concentration, the temperature of ambient air is much lower, and unlike flue gas ambient air is substantially free of corrosive contaminants.
  • the present invention addresses these problems by providing a solid material capable of reversibly adsorbing carbon dioxide, said solid material comprising a porous carrier material having deposited thereon: (i) a salt capable of reacting with carbon dioxide; and optionally (ii) a particulate, water-insoluble inorganic material.
  • Another aspect of the invention comprises a process for recovering carbon dioxide from a carbon dioxide containing gas mixture comprising (a) at a first temperature T 1 , contacting the carbon dioxide containing gas mixture with a solid material capable of reversibly adsorbing carbon dioxide; and (b) desorbing at least part of the adsorbed carbon dioxide from the solid material at a temperature T 2 , such that T 2 >T 1 and ⁇ T, defined, as T 2 minus T 1 is less than 200° C.
  • FIG. 1 is a schematic representation of a test set-up for determining the carbon dioxide absorption properties of solid materials.
  • FIG. 2 is a graph plotting the carbon dioxide desorption rates as a function of temperature for various solid materials tested in the set-up of FIG. 1 .
  • FIG. 3 is a representation of carbon dioxide loadings of various solid materials tested in the set-up of FIG. 1 .
  • FIG. 4 is a schematic representation of an absorption/desorption device for carbon dioxide and water.
  • FIG. 5 shows the device of FIG. 4 in its absorption and desorption modes.
  • FIG. 6 shows the desorption of carbon dioxide from a solid material, as a function of the desorption temperature.
  • reversibly adsorbing carbon dioxide means adsorption of carbon dioxide to a material that releases the adsorbed carbon dioxide at a temperature below 200° C.
  • the present invention relates to a solid material capable of reversibly adsorbing carbon dioxide, said solid material comprising a porous carrier material having deposited thereon: (i) a salt capable of reacting with carbon dioxide; and optionally (ii) a particulate, water-insoluble inorganic material.
  • the temperatures of adsorption and desorption are very important for the economics of the process.
  • the solid material is preferably used in a temperature swing reaction. Large temperature swings require large energy inputs. In addition, large temperature swings tend to cause deterioration of adsorbent materials.
  • the solid material is capable of adsorbing carbon dioxide at a first temperature T 1 and of desorbing carbon dioxide at a second temperature T 2 , such that T 2 >T 1 and ⁇ T, defined, as T 2 minus T 1 is less than 200° C.
  • Equations (1) and (2) illustrate an important feature of this embodiment of the invention.
  • the adsorption reaction consumes water, which is released during the desorption reaction.
  • Water needed for the adsorption reaction is typically abundantly present in the gas mixture from which carbon dioxide is being adsorbed. Flue gases are, for example, produces by burning a fossil fuel of the general formula C n H 2n+2 , the flue gas contains carbon dioxide and water in close to a 1:1 molar ratio.
  • Cold, dry air of 5° C. and 25% relative humidity contains about 0.15 mole/kg water. In all three cases there is more than enough water in the gas mixture for the adsorption reaction. In fact, it may be necessary to pre-dry the gas mixture prior to contacting it with the solid adsorbent material.
  • the adsorption/desorption process also provides water, which may be used in a subsequent CO 2 conversion reaction, or may be used in agriculture, for household use in washing and cleaning, or as a source of potable water.
  • the porous carrier material may be a honeycomb monolith material, for example of the kind as is used in catalytic converters for the treatment of exhaust gases of internal combustion engines.
  • the carrier may be made of a ceramic material, such as codierite; of a zeolite material; activated carbon; and the like.
  • the porous carrier material is made of a ceramic foam.
  • porous carrier material is activated carbon having a specific surface area in the range of from 150 m 2 /g to 600 m 2 /g.
  • the solid material contains, in addition to the porous carrier material and the reactive salt, a particulate, water-insoluble inorganic material.
  • this material is an inorganic oxide having a specific surface area of less than 100 m 2 /g.
  • the material may be derived from a corresponding material having a specific surface area in excess of 100 m 2 /g by calcination or steam calcination.
  • suitable materials include alumina, silica, titania, zirconia, ceria, clay, zeolite, layered hydroxide material, hydrotalcite, and mixtures thereof.
  • a particularly preferred example is titania.
  • Another aspect of the present invention is a process for recovering carbon dioxide from a carbon dioxide containing gas mixture comprising (a) at a first temperature T 1 , contacting the carbon dioxide containing gas mixture with a solid material capable of reversibly adsorbing carbon dioxide according to any one of the preceding claims; and (b) desorbing carbon dioxide from the solid material at least in part at a temperature T 2 , such that T 2 >T 1 and ⁇ T, defined, as T 2 minus T 1 is less than 200° C.
  • An important aspect of the invention is that a significant portion of the adsorbed CO 2 is desorbed at temperatures below 100° C.
  • the gas mixture further comprises water, such that the carbon dioxide/water molar ratio is 1:1 or less.
  • the gas mixture can be atmospheric air. It may be desirable to pre-dry atmospheric air prior to contacting it with the solid material, to adjust the carbon/dioxide/water molar ratio to within the range of from 1:1 to 1:2.
  • the adsorption temperature T 1 is preferably less than 40° C., more preferably less than 30° C.
  • the desorption temperature T 2 is preferably less than 120° C., more preferably less than 100° C.
  • T 2 is a range of temperatures at which the desorption reaction takes place. It may be desirable to increase the temperature T 2 in the course of the desorption step. For example, in the case of potassium bicarbonate on activated coal the desorption reaction can be initiated at 40° C., then slowly increased during the desorption step to 180° C. In this example the temperature T 2 is 40 to 180° C., and ⁇ T is 160° C. or less. A significant portion of the absorbed CO 2 is desorbed at temperatures below 100° C.
  • the solid material can be purged during the desorption step with an inert gas, such as nitrogen or dry steam.
  • an inert gas such as nitrogen or dry steam.
  • the first procedure was aimed at creating a wash coat-like layer in the channels of a monolith made of a material that has a low porosity.
  • the second procedure was aimed at impregnating a highly porous monolith material.
  • a suspension of an insoluble inert carrier for example TiO 2
  • a salt for CO 2 absorption for example K 2 CO 3
  • demineralized water for example K 2 CO 3
  • the mass ratios of inert:salt:demi water was used in various compositions in the range of 1:1:5 up to 2:1:1.
  • the main determining factor for the demi water content was the pore size of the monoliths to be wash coated (a lower demi water content gives a thicker solution).
  • the suspension was used to wash coat the inert monoliths, after which the monoliths were dried in an oven to remove the demi water.
  • a solution was prepared of a salt for CO 2 absorption (for example K 2 CO 3 ) in demineralized water. Mass ratios of salt:demi water in the range of 1:1 to 1:20 were used. The porous monoliths were submerged in the solution while taking that no air was trapped within the monoliths. Monoliths were then dried in the oven.
  • a salt for CO 2 absorption for example K 2 CO 3
  • Mass ratios of salt:demi water in the range of 1:1 to 1:20 were used.
  • the porous monoliths were submerged in the solution while taking that no air was trapped within the monoliths. Monoliths were then dried in the oven.
  • FIG. 1 For the development of carbon dioxide absorbing monoliths a setup was built as schematically depicted in FIG. 1 .
  • the general procedure for determining CO 2 adsorption was as follows. The air from which CO 2 is to be absorbed was supplied by an air compressor. From this air compressor the air pressure was reduced, and the air was optionally led through an air pretreatment vessel to remove excess moisture. From this air pretreatment vessel the air flowed through the CO 2 absorber and then out through the vent. After a predetermined exposure time of the CO 2 absorbent to this pretreated airflow the three way valves were switched, and the CO 2 absorber was purged with a controlled flow of nitrogen.
  • the temperature of the absorption reactor was gradually ramped up in a controlled rate while still being purged with nitrogen.
  • the composition of the outflow of the absorber was monitored by means of a CO 2 analyzer.
  • the total amount of absorbed CO 2 as a function of absorber absorption time and/or air flow rate was calculated by integrating the analyzer signal using the known flow rate of nitrogen.
  • FIGS. 2 and 3 An example of results of this experimental setup are shown in FIGS. 2 and 3 (these results were obtained with impregnated carbon dioxide absorbing honeycomb monoliths impregnated with K 2 CO 3 in 1:10 solution (1 part K 2 CO 3 to 10 parts water)).
  • adsorption was done at ambient temperature, desorption up to 180° C.
  • the CO 2 concentration in the outflow of the absorber as measured by the CO 2 analyzer is plotted as a function of the core temperature of the absorber. It can be seen that the release of CO 2 started immediately when heating of the absorbent was commenced. Maximum desorption of CO 2 occurred around 100° C., and high desorption rates occurred between 100° C. and about 140° C. Release of CO 2 ceased around 180° C.
  • the maximum CO 2 concentration desorbed by the monoliths increases when exposure time to air previous to the desorption sequence increases.
  • the maximum CO 2 concentration desorbed was about 18000 ppm.
  • a 2 hour exposure time resulted in the maximum CO 2 concentration (ppm) desorbed being less than 40000 ppm, about 38500-39000 ppm.
  • the maximum CO 2 concentration desorbed was about 47000 ppm.
  • the maximum CO 2 concentration desorbed was about 49000 ppm.
  • the maximum CO 2 concentration desorbed was about 49500 ppm.
  • the maximum CO 2 concentration desorbed was about 50000 ppm. With an exposure time of 20 hours, the maximum CO 2 concentration desorbed was just under 50000 ppm, indicating that the exposure time at which most CO 2 is desorbed is above 14 hours.
  • FIG. 3 the total amount of CO 2 released as a function of absorbent exposure time to airflow is shown. This is shown for three samples of monoliths: a sample that was not impregnated, a sample that was impregnated with a 1:20 solution of potassium carbonate (by mass) and a sample that was impregnated with a 1:10 solution of potassium carbonate (by mass). It can be seen that unimpregnated samples do not absorb CO 2 . The samples impregnated with the 1:10 solution impregnation absorbed more CO 2 than the 1:20 impregnation. Furthermore the absorber appears to be saturated after an exposure to air of approximately 8 hours. After this time the amount of absorbed CO 2 no longer increased.
  • the absorbent material is used for capturing carbon dioxide and water from air in arid regions, such as deserts. As illustrated above in paragraph
  • a column filled with absorbent material will absorb water and carbon dioxide from cold desert air during the night. During the day the heat of the sun will raise the temperature of the column high enough to cause the water and carbon dioxide to desorb. Desorbed water and carbon dioxide can be stored in a storage vessel. Both can be used in a greenhouse to supply growing plants with two essential ingredients for the photosynthetic process.
  • the need for water in this embodiment is greater than the need for carbon dioxide.
  • the column can be partly filled with a desiccant, such as silica gel, and partly with the absorbent material of the invention.
  • the desiccant can be placed upstream or downstream from the CO 2 absorbent.
  • air can be forced through the column by mechanical means, such as a fan. It is possible also to use the natural temperature differences for creating the required air flow. This is illustrated in FIGS. 4 and 5 .
  • FIG. 4 shows a column 10 , containing absorbent material.
  • Column 10 preferably has a rectangular cross section, with a heat capturing surface 11 preferably having an orientation for optimum solar exposure, i.e., a predominantly southern exposure in the northern hemisphere, or a predominantly northern exposure in the southern hemisphere.
  • FIG. 4 shows the column in its open configuration.
  • solar collector 14 captures solar heat, which heats op oil present in solar collector 14 .
  • Expansion of the oil caused by the increase in temperature raises the pressure in solar collector 14 and oil lines 15 and 16 .
  • the oil pressure is used to move bottom plate 12 and desorption head 13 to their closed positions.
  • the temperature of the oil drops, the oil pressure drops, and bottom plate 12 and desorption head 13 move to their open positions.
  • FIG. 5 shows, on the left hand side, column 10 in its night time (open) configuration.
  • the rapid drop in ambient temperature causes a downward air flow through column 10 , allowing the absorber to absorb water and carbon dioxide from the air.
  • Column 10 in the right hand portion of FIG. 5 shows the daytime (closed) configuration. Column 10 and its contents are heated up by the sun. This effect is amplified by having heat exchange surface 11 oriented to the sun. Although the ambient temperature rarely exceeds 40° C. (measured in the shade), the temperature of the absorbent material inside column 10 may reach or even exceed 100° C. Water and carbon dioxide absorbed to the absorbent material are desorbed at these temperatures.
  • Solar heat also causes an upward gas flow inside column 10 , so that desorbing gases are collected in desorption head 13 , and from there in storage vessel 17 .
  • Storage vessel 17 may be located in a cool place, for example underground. The temperature difference between column 10 and storage vessel 17 reinforces the gas flow. Moreover, a significant portion of the desorbed water collected in storage vessel 17 is condensed to liquid water.
  • column 10 is not purged when it changes over from absorption mode to desorption mode.
  • storage vessel contains air components, such as nitrogen and oxygen, in addition to carbon dioxide and water. If the contents of storage vessel are to be used in a greenhouse for growing plants, the presence of oxygen and nitrogen is of course not harmful.
  • the desorption behavior of an exemplary absorbent material was determined in the following experiment.
  • the absorbent material was an active carbon honeycomb, impregnated with K 2 CO 3 .
  • the material was saturated with carbon dioxide by prolonged exposure to air. Then the material was flushed with nitrogen, while the temperature was increased in steps of 20° C. After each temperature increase the temperature was kept constant until no carbon dioxide was detectable anymore in the nitrogen flow leaving the absorbent bed.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Drying Of Gases (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
US14/415,147 2012-07-17 2013-07-17 Materials and process for reversible adsorption of carbon dioxide Abandoned US20150139887A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US14/415,147 US20150139887A1 (en) 2012-07-17 2013-07-17 Materials and process for reversible adsorption of carbon dioxide

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US201261672333P 2012-07-17 2012-07-17
US14/415,147 US20150139887A1 (en) 2012-07-17 2013-07-17 Materials and process for reversible adsorption of carbon dioxide
PCT/EP2013/065070 WO2014012963A1 (fr) 2012-07-17 2013-07-17 Matériaux et procédé pour l'adsorption réversible du dioxyde de carbone

Publications (1)

Publication Number Publication Date
US20150139887A1 true US20150139887A1 (en) 2015-05-21

Family

ID=48803538

Family Applications (2)

Application Number Title Priority Date Filing Date
US14/415,149 Active 2033-09-03 US9550142B2 (en) 2012-07-17 2013-07-17 Device for temperature swing process
US14/415,147 Abandoned US20150139887A1 (en) 2012-07-17 2013-07-17 Materials and process for reversible adsorption of carbon dioxide

Family Applications Before (1)

Application Number Title Priority Date Filing Date
US14/415,149 Active 2033-09-03 US9550142B2 (en) 2012-07-17 2013-07-17 Device for temperature swing process

Country Status (7)

Country Link
US (2) US9550142B2 (fr)
EP (1) EP2874727B1 (fr)
AU (1) AU2013292078B2 (fr)
CA (1) CA2883058A1 (fr)
ES (1) ES2662006T3 (fr)
NO (1) NO2905335T3 (fr)
WO (1) WO2014012966A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160157438A1 (en) * 2012-07-17 2016-06-09 Antecy B.V. Method for accelerating growth of plants in a controlled environment
WO2018150582A1 (fr) * 2017-02-20 2018-08-23 日立化成株式会社 Appareil de conditionnement d'air et système de conditionnement d'air
WO2018150583A1 (fr) * 2017-02-20 2018-08-23 日立化成株式会社 Climatiseur et système de climatisation
US11612879B2 (en) * 2017-11-10 2023-03-28 Climeworks Ag Materials for the direct capture of carbon dioxide from atmospheric air

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2734786C (fr) 2008-08-21 2017-11-07 Carbon Engineering Limited Partnership Procede et unite de capture de dioxyde de carbone
CN105992630B (zh) 2013-12-03 2019-03-15 安特西有限公司 水分摆动二氧化碳富集方法
WO2016005226A1 (fr) * 2014-07-10 2016-01-14 Climeworks Ag Procédé de désorption sous vide assistée par de la vapeur pour capturer du dioxyde de carbone
CA2970687A1 (fr) 2016-06-14 2017-12-14 Carbon Engineering Limited Partnership Captage de dioxyde de carbone
EP3482813A1 (fr) 2017-11-13 2019-05-15 Antecy Dispositif de capture et de concentration efficaces de co2 à partir de flux gazeux dans un lit radial
US11420149B2 (en) 2018-06-14 2022-08-23 Climeworks Ag Efficient method and device for adsorption/desorption of carbon dioxide from gas streams
EP3614059A1 (fr) 2018-08-23 2020-02-26 Antecy B.V. Procédé et dispositif pour améliorer la qualité de l'air dans des environnements fermés
US11446605B2 (en) 2019-11-15 2022-09-20 Carbon Capture Approach to cost effective carbon capture from air by producing carbon negative water
EP4157485A1 (fr) 2020-05-27 2023-04-05 Climeworks AG Désorption de vapeur atmosphérique pour la capture directe d'air
WO2021239749A1 (fr) 2020-05-27 2021-12-02 Climeworks Ag Procédés et dispositif pour la capture de dioxyde de carbone entrainée par la vapeur
WO2021239747A1 (fr) 2020-05-29 2021-12-02 Climeworks Ag Procédé de capture de dioxyde de carbone à partir d'air ambiant et structures adsorbantes correspondantes avec une pluralité de surfaces parallèles
GB2592707B (en) * 2020-11-26 2022-03-30 Provost Fellows Found Scholars & Other Members Board College Holy & Und Providing heat energy to direct air carbon dioxide capture processes using waste heat from data centre
US20230233989A1 (en) * 2022-01-26 2023-07-27 Battelle Memorial Institute System and method for direct air capture of water and co2
WO2024039641A1 (fr) 2022-08-15 2024-02-22 W. L. Gore & Associates, Inc. Structures et procédés pour améliorer la capture de dioxyde de carbone de l'air ambiant

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8840706B1 (en) * 2011-05-24 2014-09-23 Srivats Srinivasachar Capture of carbon dioxide by hybrid sorption

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4344778A (en) * 1979-05-15 1982-08-17 Mitsubishi Denki Kabushiki Kaisha Water producing apparatus
DE3415970A1 (de) * 1984-04-28 1985-10-31 Walter 6239 Kriftel Fabinski Verfahren zum sammeln und speichern von kohlendioxid
US4784672A (en) * 1987-10-08 1988-11-15 Air Products And Chemicals, Inc. Regeneration of adsorbents
US6863711B2 (en) * 2002-12-06 2005-03-08 Hamilton Sundstrand Temperature swing humidity collector using powerplant waste heat
DE10338418B4 (de) * 2003-08-18 2009-01-22 Donau Carbon Gmbh & Co. Kg Verfahren und Anlage zur Abgasreinigung
US20070051238A1 (en) * 2005-09-07 2007-03-08 Ravi Jain Process for gas purification
US8591627B2 (en) * 2009-04-07 2013-11-26 Innosepra Llc Carbon dioxide recovery
US8167978B2 (en) * 2008-10-09 2012-05-01 Pratt & Whitney Rocketdyne, Inc. Gas generator and method therefor
US8840704B2 (en) * 2009-07-27 2014-09-23 Kawasaki Jukogyo Kabushiki Kaisha Carbon dioxide separation method and apparatus
CN103140273B (zh) * 2010-01-22 2016-06-08 新加坡国立大学 除湿器和除湿方法

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8840706B1 (en) * 2011-05-24 2014-09-23 Srivats Srinivasachar Capture of carbon dioxide by hybrid sorption

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160157438A1 (en) * 2012-07-17 2016-06-09 Antecy B.V. Method for accelerating growth of plants in a controlled environment
WO2018150582A1 (fr) * 2017-02-20 2018-08-23 日立化成株式会社 Appareil de conditionnement d'air et système de conditionnement d'air
WO2018150583A1 (fr) * 2017-02-20 2018-08-23 日立化成株式会社 Climatiseur et système de climatisation
US11612879B2 (en) * 2017-11-10 2023-03-28 Climeworks Ag Materials for the direct capture of carbon dioxide from atmospheric air

Also Published As

Publication number Publication date
CA2883058A1 (fr) 2014-01-23
EP2874727A1 (fr) 2015-05-27
US20150182904A1 (en) 2015-07-02
EP2874727B1 (fr) 2017-12-06
NO2905335T3 (fr) 2018-06-30
ES2662006T3 (es) 2018-04-05
AU2013292078B2 (en) 2017-12-14
WO2014012966A1 (fr) 2014-01-23
AU2013292078A1 (en) 2015-01-29
US9550142B2 (en) 2017-01-24

Similar Documents

Publication Publication Date Title
US20150139887A1 (en) Materials and process for reversible adsorption of carbon dioxide
EP2874728A1 (fr) Matériaux et procédé pour l'adsorption réversible du dioxyde de carbone
Lee et al. Dry potassium-based sorbents for CO 2 capture
Lee et al. The effect of water on the activation and the CO 2 capture capacities of alkali metal-based sorbents
Rezaei et al. SO x/NO x removal from flue gas streams by solid adsorbents: a review of current challenges and future directions
Drage et al. Materials challenges for the development of solid sorbents for post-combustion carbon capture
AU2010277084B2 (en) Carbon Dioxide Separation Method and Apparatus
Lee et al. CO2 absorption and regeneration of alkali metal-based solid sorbents
Kong et al. Research needs targeting direct air capture of carbon dioxide: Material & process performance characteristics under realistic environmental conditions
Manovic et al. Reactivation and remaking of calcium aluminate pellets for CO2 capture
US20060039853A1 (en) Separation of carbon dioxide (CO2) from gas mixtures by calcium based reaction separation (CaRS-CO2) process
Santillán-Reyes et al. Analysis of the CO2 capture in sodium zirconate (Na2ZrO3). Effect of the water vapor addition
SA111320418B1 (ar) نظام وطريقة لاحتجاز ثاني أكسيد الكربون وتنحية أيوناته
Yu et al. Al 2 O 3 and CeO 2-promoted MgO sorbents for CO 2 capture at moderate temperatures
CA2785323A1 (fr) Absorbant de co2
Lee et al. Effects of alumina phases on CO 2 sorption and regeneration properties of potassium-based alumina sorbents
Madzaki et al. Carbon dioxide adsorption on activated carbon hydrothermally treated and impregnated with metal oxides
US9144770B2 (en) Reversible sorbent for warm CO2 capture by pressure swing adsorption
Puccini et al. Removal of CO2 from flue gas at high temperature using novel porous solids
Goldman et al. Parametric and laboratory aging studies of direct CO2 air capture simulating ambient capture conditions and desorption of CO2 on supported alkaline adsorbents
KR101502238B1 (ko) 이산화탄소 흡수제 및 이를 이용한 이산화탄소 흡수 공정
CN112316902A (zh) 一种复合MgO吸附剂及其制备方法与应用
Puccini et al. The effect of flue gas contaminants on CO2 capture at high temperature by Li4SiO4-based sorbents
Shelyapina et al. Materials for CO 2, SO x, and NO x Emission Reduction
CN102430384B (zh) 高活性无机-无机烟气co2吸附剂及其制备方法

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION