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WO2025062000A1 - Procédé et dispositif de production continue de dioxyde de carbone à partir d'une atmosphère gazeuse contenant du dioxyde de carbone - Google Patents

Procédé et dispositif de production continue de dioxyde de carbone à partir d'une atmosphère gazeuse contenant du dioxyde de carbone Download PDF

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Publication number
WO2025062000A1
WO2025062000A1 PCT/EP2024/076519 EP2024076519W WO2025062000A1 WO 2025062000 A1 WO2025062000 A1 WO 2025062000A1 EP 2024076519 W EP2024076519 W EP 2024076519W WO 2025062000 A1 WO2025062000 A1 WO 2025062000A1
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WO
WIPO (PCT)
Prior art keywords
carbon dioxide
liquid sorbent
gas stream
containing gas
sorbent
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.)
Pending
Application number
PCT/EP2024/076519
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German (de)
English (en)
Inventor
Ulrich ZUBERBÜHLER
Sebastian Thaler
Raphael Vollmer
Dominik ROTH
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.)
Zentrum fuer Sonnenenergie und Wasserstoff Forschung Baden Wuerttemberg
Original Assignee
Zentrum fuer Sonnenenergie und Wasserstoff Forschung Baden Wuerttemberg
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Filing date
Publication date
Application filed by Zentrum fuer Sonnenenergie und Wasserstoff Forschung Baden Wuerttemberg filed Critical Zentrum fuer Sonnenenergie und Wasserstoff Forschung Baden Wuerttemberg
Publication of WO2025062000A1 publication Critical patent/WO2025062000A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • B01D53/14—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
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • B01D53/14—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
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20415—Tri- or polyamines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
    • 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
    • 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

  • Low-temperature processes which are typically carried out at a desorption temperature of approximately 100°C, predominantly utilize short-chain, solid-bound amines such as monoethanolamine (MEA), diethanolamine (DEA), or methyldiethanolamine (MDEA) as sorbents.
  • MEA monoethanolamine
  • DEA diethanolamine
  • MDEA methyldiethanolamine
  • the low desorption temperature of approximately 100°C is typically achieved by setting a negative pressure in the desorption unit (hereinafter referred to as the desorber), which severely limits its installation space. Since adsorption and desorption are separated only temporally and not spatially, this also affects the absorption unit (hereinafter referred to as the absorber).
  • the high-temperature processes are based on the use of aqueous alkali or alkaline earth metal hydroxide solutions as sorbents and can therefore be designed as continuous processes.
  • the use of aqueous alkali or alkaline earth metal hydroxide solutions requires desorption temperatures of up to 900°C.
  • natural gas is usually burned, which leads to the release of new carbon dioxide.
  • the desorption cycle which involves several chemical conversion processes, is technically complex and cost-intensive, and that, in contrast to low-temperature processes, no waste heat from low-temperature processes such as electrolysis or methanation can be incorporated.
  • the object underlying the present invention was to provide a process and a device for the continuous recovery of carbon dioxide from a carbon dioxide-containing gas atmosphere, which at least partially overcomes the disadvantages of the prior art.
  • the process should be particularly energy-efficient and cost-effective by combining the advantages of known low-temperature processes with the advantages of known high-temperature processes.
  • EP 2700440 A2 and DE 102004053 167 A1 each disclose a method and a system for the continuous recovery of carbon dioxide from a flue gas stream generated by the combustion of fuel.
  • the methods comprise an absorption step, which comprises continuously contacting the flue gas stream with a liquid sorbent in a countercurrent manner, whereby the liquid sorbent absorbs carbon dioxide and forms a carbon dioxide-laden liquid sorbent and a carbon dioxide-depleted flue gas stream, and a desorption step comprising continuously heating the carbon dioxide-laden liquid sorbent, whereby the carbon dioxide-laden liquid sorbent desorbs carbon dioxide and regenerates the liquid sorbent.
  • an absorption step comprising continuously contacting a carbon dioxide-containing gas stream with a liquid sorbent in a countercurrent or cross-current manner at ambient temperature and under atmospheric pressure, whereby the liquid sorbent absorbs carbon dioxide and forms a carbon dioxide-laden liquid sorbent and a carbon dioxide-depleted gas stream;
  • the liquid sorbent used in the present invention is a sorbent comprising polyethyleneimine (PEI) as an essential component.
  • PEI polyethyleneimine
  • Polyethylenimines are polymers formally obtained by polymerizing ethyleneimine (aziridine) and containing a large number of amino groups. Due to their strongly basic properties, polyethyleneimines are usually present as polycations, which makes them highly soluble in water and other protic solvents. At the same time, polyethyleneimines generally have a number-average molecular weight of at least several thousand g/mol, resulting in a relatively low vapor pressure. This represents a significant advantage over the short-chain amines known, for example, from flue gas scrubbing, since high air volume flows are required for the direct recovery of carbon dioxide from ambient air.
  • the number-average molecular weight of the polyethyleneimine is not particularly limited, but is preferably in a range from 1000 to 200,000 g/mol, more preferably 2500 to 150,000 g/mol, and most preferably 5000 to 100,000 g/mol, as determined by gel permeation chromatography.
  • Suitable polyethyleneimines are known in the art and are commercially available from Alfa Aesar, Sigma-Aldrich and TCI Chemical, among others.
  • the concentration of polyethyleneimine in the liquid sorbent is usually in a range from 5 to 35 wt.%, and preferably in a range from 10 to 25 wt.%, based on the total weight of the liquid sorbent.
  • the process according to the invention can be operated continuously without any problems and without any special technical effort.
  • the process according to the invention achieves a significant advantage of known low-temperature processes, namely that of a low desorption temperature of carbon dioxide. This allows the absorption and desorption steps to be spatially separated from one another and individually adapted to the respective conditions. This is important because an absorber used in the absorption step must be as large as possible due to the high gas volume flow, while a desorber used in the desorption step should be as small as possible with a view to reducing energy consumption.
  • standard pressure refers to the air pressure prevailing at the respective location during implementation of the process. If the process is carried out at sea level, for example, the standard pressure is 1013.25 hPa or approximately 1 bar. If the process is carried out at 1000 m above sea level, the standard pressure drops to 891 hPa.
  • Adequate absorption of carbon dioxide during the absorption step is achieved by bringing the carbon dioxide-containing gas stream into contact with the liquid sorbent using the countercurrent or crosscurrent principle (see Fig. 8).
  • a countercurrent absorber offers numerous advantages over a crosscurrent absorber. These advantages include higher absorption efficiency, as the carbon dioxide-containing gas stream to be purified and the liquid sorbent flow in opposite directions, thus creating a maximum concentration difference within the absorber, and the concentration difference is the driving force for the absorption reaction. Further advantages include better mass transfer (since the continuous collision of the carbon dioxide-containing gas stream and the liquid sorbent over the entire length of the absorber continually creates new phase interfaces between gas and liquid), a lower risk of channeling, and easier aerosol separation.
  • a demister can be used, for example, within the scope of the process according to the invention, whereby such a demister can easily drip downwards when the countercurrent principle is applied.
  • a slow flow of the carbon dioxide-containing gas stream through the absorber is aimed for.
  • the latter implies a reduction of the Flow velocity, which is why the inflow area of the absorber ultimately has to be enlarged and, when the counterflow principle is used, a larger area is required.
  • a cross-flow absorber offers the advantage of better use of floor space compared to a counterflow absorber, since the inflow area can be extended vertically.
  • a generally cylindrical counterflow absorber develops into a rather flat and rectangular cross-flow absorber, which can better utilize natural air movement due to its orientation in the prevailing wind direction than a counterflow absorber.
  • the absorption step it is therefore preferred according to the invention for the absorption step to comprise the continuous contacting of the carbon dioxide-containing gas stream with the liquid sorbent using the cross-flow principle, even though the use of a cross-flow absorber at first glance entails disadvantages compared to the use of a counterflow absorber.
  • a device designed to carry out the process according to the invention therefore comprises at least one absorber, one desorber, one feed line for a carbon dioxide-containing gas stream, one feed line for a liquid solvent, one A supply line for a liquid sorbent, a discharge line for a carbon dioxide-depleted gas stream, a discharge line for a carbon dioxide-laden liquid sorbent, and a carbon dioxide discharge line.
  • this comprises the continuous contacting of the carbon dioxide-containing gas stream with the liquid sorbent using the cross-flow principle.
  • a cross-flow absorber designed as a wall module solves the problem of the high floor space requirement of a counter-flow absorber, new challenges arise in connection with gas conveyance and particle separation. For example, to convey the carbon dioxide-containing gas stream upstream of the packing and to separate unwanted particles downstream of the packing, the entire inflow area of a cross-flow absorber must be covered, which requires a high use of material and components.
  • the absorption step of the process according to the invention particularly comprises Preferably, in addition, the carbon dioxide-depleted gas stream is discharged in a direction substantially perpendicular to the flow direction of the carbon dioxide-containing gas stream during absorption and in a direction opposite to the flow direction of the liquid sorbent during absorption.
  • the carbon dioxide-depleted gas stream be sucked out of the absorber in a suitable manner.
  • the absorber can be configured such that it is uniformly supplied with carbon dioxide-containing gas over its entire surface area (i.e., the carbon dioxide-containing gas is sucked in over the entire surface area) and simultaneously enables efficient removal of the carbon dioxide-depleted gas.
  • this is preferably achieved by the means for discharging the carbon dioxide-depleted gas stream from the absorber comprising a gas channel and a fan connected to the gas channel, the gas channel being spatially arranged around the longitudinal axis of the absorber, and the gas channel being surrounded by the means for continuously contacting the carbon dioxide-containing gas stream with the liquid aqueous sorbent in a cross-flow manner.
  • a large phase interface is also advantageous, for which random packings or packings are generally used in combination with spray nozzles or distribution channels. While spray nozzles consume a great deal of energy due to the upstream pressure, distribution channels tend to result in an inhomogeneous distribution of the scrubbing liquid.
  • the desorption step can comprise the continuous heating of the carbon dioxide-laden liquid sorbent to a temperature higher than ambient temperature.
  • the desorption step comprises the continuous heating of the carbon dioxide-laden liquid sorbent to a temperature higher than ambient temperature
  • providing the temperature higher than ambient temperature preferably comprises the transfer of thermal energy from the liquid sorbent of the desorption step to the carbon dioxide-laden liquid sorbent of the absorption step.
  • a device configured to carry out the method according to the invention therefore further comprises, in addition to the aforementioned components, a means connected to the absorber and the desorber for transferring thermal energy from the absorber to the desorber, wherein the means is preferably a high-temperature heat pump.
  • providing the carbon dioxide partial pressure reduced compared to normal pressure preferably comprises reducing the absolute pressure and/or mixing the carbon dioxide-laden liquid sorbent with at least one stripping gas, with the simultaneous reduction of the absolute pressure and mixing of the carbon dioxide-laden liquid sorbent with at least one stripping gas being considered particularly preferred.
  • a device configured to carry out the method according to the invention consequently comprises a desorber which, in addition to the aforementioned components, further comprises means for reducing the absolute pressure and/or means for mixing the carbon dioxide-laden liquid sorbent with at least one stripping gas.
  • the absolute pressure By reducing the absolute pressure or setting a negative pressure specific to the respective location, the temperature required for evaporation of the liquid sorbent can be lowered, thus reducing the energy required for the desorption step. This allows, among other things, high-temperature heat pumps to be used as a heat source. Since the generation of negative pressure also consumes energy, the absolute pressure is preferably selected such that an energetic optimum is achieved between the energy required for a pressure reduction and the energy saved by a temperature reduction.
  • Stripping gases which are suitable for use in the process according to the invention and which are fed into a device configured to carry out the process according to the invention via a line connected to a second inlet opening of the desorber Stripping gas feed lines that can be introduced into the desorber are known in the art and include, among others, air, steam, hydrogen, and nitrogen.
  • the stripping gas is preferably steam, hydrogen, nitrogen, or a mixture thereof, the advantage of using steam being that the water contained in the product gas stream can be condensed out without great difficulty.
  • a disadvantage is the high enthalpy of vaporization required to heat the liquid sorbent and to generate steam from liquid water.
  • the process according to the invention particularly preferably furthermore enables the transfer of thermal energy from the product gas stream of the desorption step to the liquid sorbent of the absorption step and/or to liquid water, which is to be fed to the carbon dioxide-laden liquid sorbent in the form of steam as stripping gas during the desorption step.
  • a device configured to carry out the method according to the invention therefore further comprises, in addition to the aforementioned components, a means connected to the carbon dioxide discharge line and the liquid sorbent feed line for transferring thermal energy from the product gas stream to the liquid sorbent (to be fed to the absorber), and/or a means connected to the carbon dioxide discharge line and the stripping gas feed line for transferring thermal energy from the product gas stream to liquid water, wherein the means is preferably a high-temperature heat pump. If hydrogen or nitrogen is used as the stripping gas, the thermal energy required to generate steam is reduced.
  • the appropriate ratio of carbon dioxide and stripping gas in particular hydrogen
  • the appropriate ratio of carbon dioxide and stripping gas can be set in advance depending on the type of downstream process, which significantly reduces the technical effort required for purifying the product gas stream.
  • a device configured to carry out the method according to the invention comprises In addition to the aforementioned components, the device therefore further comprises a means connected to the carbon dioxide discharge line and the stripping gas supply line for at least partially separating stripping gas from the desorbed carbon dioxide, wherein the means is preferably a membrane.
  • the product gas stream obtained in the desorption step can, for example, be fed to a downstream condensate separator and/or a downstream membrane (if hydrogen or nitrogen is used as the stripping gas), wherein the stripping gas is separated from desorbed carbon dioxide and pumped back to the desorber via appropriately configured lines.
  • a downstream condensate separator and/or a downstream membrane if hydrogen or nitrogen is used as the stripping gas
  • the stripping gas is separated from desorbed carbon dioxide and pumped back to the desorber via appropriately configured lines.
  • the desorption step of the method according to the invention preferably further comprises providing the carbon dioxide-laden liquid sorbent as a film with a film thickness of less than 3 mm, and particularly preferably less than 1 mm.
  • a device configured to carry out the method according to the invention consequently comprises a desorber which, in addition to the aforementioned components, further comprises a means for providing the carbon dioxide-laden liquid sorbent as a film with a film thickness of less than 1 mm, wherein the means is preferably a thin-film evaporator.
  • the process according to the invention may comprise one or more additional steps, such as a filtration step, a pre-washing step, a gas conditioning step, and a control step.
  • the process according to the invention preferably further comprises a Filtration step, which comprises filtering the carbon dioxide-containing gas stream prior to the absorption step.
  • a device configured to carry out the method according to the invention in addition to the aforementioned components, further comprises a means for filtering the carbon dioxide-containing gas stream, which means is connected to the supply line for a carbon dioxide-containing gas stream and the first inlet opening of the absorber.
  • the means is preferably a dust or pollen filter, which prevents the entry of coarse contaminants into the scrubbing liquid.
  • the process according to the invention preferably further comprises a pre-washing step, which involves pre-washing the carbon dioxide-containing gas stream with water before the absorption step, wherein the water is preferably decalcified water.
  • DI water demineralized water
  • a device configured to carry out the method according to the invention therefore further comprises, in addition to the aforementioned components, a means for pre-washing the carbon dioxide-containing gas stream with water, which means is connected to the supply line for a carbon dioxide-containing gas stream and the first inlet opening of the absorber or is integrated into the absorber.
  • the means is preferably a gas pre-washer. The gas pre-wash achieves both a reduction in the amount of deionized water required and an additional filter function, and can be maintained by cyclical replacement of the washing liquid.
  • the process according to the invention can alternatively comprise a gas conditioning step, which comprises recovering liquid solvent from the carbon dioxide-depleted gas stream after the desorption step and humidifying the carbon dioxide-containing gas stream with the recovered liquid solvent before the absorption step.
  • a A device configured to carry out the method according to the invention in addition to the components mentioned above, therefore further comprises a means connected to the supply line for a carbon dioxide-containing gas stream and the discharge line for a carbon dioxide-depleted gas stream for recovering liquid solvent from the carbon dioxide-depleted gas stream and for humidifying the carbon dioxide-containing gas stream with the recovered liquid solvent, wherein the means is preferably a sorption wheel.
  • a sorption wheel If the supply air and the exhaust air of the absorber are connected to one another via a sorption wheel or a rotary dehumidifier, moisture as well as heat can be transferred, since the sorption wheel is coated with a hygroscopic material such as silica gel or zeolite. Compared to the use of a gas pre-scrubber described above, a sorption wheel also offers the advantage that not only the amount of deionized water used but also the overall water consumption of the device can be reduced.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé de production en continu de dioxyde de carbone à partir d'une atmosphère gazeuse contenant du dioxyde de carbone, qui peut facilement être développé et peut être mis en œuvre de manière particulièrement efficace sur le plan énergétique et économique, ainsi qu'un dispositif pour la mise en œuvre de ce procédé. Le procédé comprend (a) une étape d'absorption qui comprend la mise en contact continue d'un flux gazeux contenant du dioxyde de carbone avec un sorbant liquide selon le principe du contre-courant ou du courant croisé à température ambiante et sous pression normale, le sorbant liquide absorbant le dioxyde de carbone et un sorbant liquide chargé de dioxyde de carbone ainsi qu'un flux gazeux appauvri en dioxyde de carbone étant formés ; et (b) une étape de désorption qui comprend le chauffage continu du sorbant liquide chargé en dioxyde de carbone à une température élevée par rapport à la température ambiante ou/et le passage continu du sorbant liquide chargé de dioxyde de carbone à travers une atmosphère présentant une pression partielle de dioxyde de carbone réduite par rapport à la pression normale, le sorbant liquide chargé de dioxyde de carbone désorbant le dioxyde de carbone et le sorbant liquide étant régénéré. Le procédé est en outre caractérisé en ce que le sorbant liquide comprend du polyéthylène imine.
PCT/EP2024/076519 2023-09-21 2024-09-20 Procédé et dispositif de production continue de dioxyde de carbone à partir d'une atmosphère gazeuse contenant du dioxyde de carbone Pending WO2025062000A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102023125666.1 2023-09-21
DE102023125666.1A DE102023125666A1 (de) 2023-09-21 2023-09-21 Verfahren und Vorrichtung zur kontinuierlichen Gewinnung von Kohlenstoffdioxid aus einer kohlenstoffdioxidhaltigen Gasatmosphäre

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Publication Number Publication Date
WO2025062000A1 true WO2025062000A1 (fr) 2025-03-27

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PCT/EP2024/076519 Pending WO2025062000A1 (fr) 2023-09-21 2024-09-20 Procédé et dispositif de production continue de dioxyde de carbone à partir d'une atmosphère gazeuse contenant du dioxyde de carbone

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WO (1) WO2025062000A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5376614A (en) * 1992-12-11 1994-12-27 United Technologies Corporation Regenerable supported amine-polyol sorbent
DE102004053167A1 (de) 2004-11-01 2006-05-04 Degussa Ag Polymere Absorptionsmittel für die Gasabsorption und Absorptionsprozess
EP2700440A2 (fr) 2012-08-24 2014-02-26 Alstom Technology Ltd Procédé et système de capture de CO2 à partir d'un flux et solvants utilisés dans celui-ci
WO2023043843A1 (fr) * 2021-09-14 2023-03-23 Carbon Engineering Ltd. Capture de dioxyde de carbone
US20230130721A1 (en) * 2021-10-27 2023-04-27 Ut-Battelle, Llc Intensified carbon capture using building infrastructure

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5376614A (en) * 1992-12-11 1994-12-27 United Technologies Corporation Regenerable supported amine-polyol sorbent
DE102004053167A1 (de) 2004-11-01 2006-05-04 Degussa Ag Polymere Absorptionsmittel für die Gasabsorption und Absorptionsprozess
EP2700440A2 (fr) 2012-08-24 2014-02-26 Alstom Technology Ltd Procédé et système de capture de CO2 à partir d'un flux et solvants utilisés dans celui-ci
WO2023043843A1 (fr) * 2021-09-14 2023-03-23 Carbon Engineering Ltd. Capture de dioxyde de carbone
US20230130721A1 (en) * 2021-10-27 2023-04-27 Ut-Battelle, Llc Intensified carbon capture using building infrastructure

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
FASIHI ET AL., J. CLEAN. PROD., vol. 224, pages 957 - 980
HESS ET AL.: "Studie im Auftrag des Ministeriums für Verkehr Baden-Württemberg", December 2020, KARLSRUHE INSTITUTE OF TECHNOLOGY, article "Nutzung von CO aus Luft als Rohstoff für synthetische Kraftstoffe und Chemikalien"
VIEHBAHN, ENERGIEWIRTSCH. TAGESFRAGEN, vol. 69, no. 12, pages 30 - 33

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