WO2014127410A1 - Procédé de régénération d'un absorbant pour la capture de dioxyde de carbone - Google Patents

Procédé de régénération d'un absorbant pour la capture de dioxyde de carbone Download PDF

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Publication number
WO2014127410A1
WO2014127410A1 PCT/AU2014/000142 AU2014000142W WO2014127410A1 WO 2014127410 A1 WO2014127410 A1 WO 2014127410A1 AU 2014000142 W AU2014000142 W AU 2014000142W WO 2014127410 A1 WO2014127410 A1 WO 2014127410A1
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WIPO (PCT)
Prior art keywords
carbon dioxide
solvent
liquid solvent
rich liquid
heating
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Ceased
Application number
PCT/AU2014/000142
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English (en)
Inventor
Rajab KHALILPOUR
Abdul Qadir
Ali Abbas
Matteo Chiesa
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University of Sydney
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University of Sydney
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Filing date
Publication date
Priority claimed from AU2013900549A external-priority patent/AU2013900549A0/en
Application filed by University of Sydney filed Critical University of Sydney
Publication of WO2014127410A1 publication Critical patent/WO2014127410A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • 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
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention relates to a method of regenerating a solvent used in the absorption of carbon dioxide from a flue gas, and in particular to a method of regenerating a solvent using solar energy.
  • Carbon-based fossil fuel resources comprise today about 86% of global primary energy and they are said to be a major contributor to global warming. Power plant, transportation, and industry converted this fuel into approximately 29 billion metric tonnes CO 2 in 2006 while this is expected to grow to 33.1 and 40.4 billion metric tonnes CO 2 by 2015 and 2030, respectively (EIA, 2009).
  • the recent Copenhagen meeting on climate change highlighted a frantic need to reduce global emissions so as to hold the increase in global temperature below 2 degrees Celsius (equivalent to 450 parts per million of CC ⁇ ) (UNFCCC, 2009).
  • World Energy Outlook 2009 (IEA, 2009) estimated that capping atmospheric temperature rise below 2°C by 2030 requires avoiding of C0 2 at 3.8 and 13.8 billion metric tonnes by 2020 and 2030, respectively. This represents a significant escalation in C0 2 abatement. Such a goal requires an additional US$10.5 trillion of cumulative energy-related investment.
  • the main options for reducing carbon emissions are: (1) reduction of energy usage, e.g. via efficiency improvement, (2) replacing fossil fuels by zero or reduced carbon-emitting sources, such as renewable, biofuels and nuclear, and (3) capture and storage of C0 2 .
  • renewable energy sources such as renewable, biofuels and nuclear
  • capture and storage C0 2 .
  • solvent and membrane technologies seem to be the most reliable in the medium term.
  • Post-combustion carbon capture from flue gas is well understood and is currently used in different industrial applications.
  • PCC started in the 1970s, not with the concern for its global warming effect, but as a potential economic source of C0 2 , mainly for enhanced oil recovery (EO ) operations.
  • EO enhanced oil recovery
  • solvent-based PCC is almost ready today while other PCC technologies (membrane, adsorption, etc.), pre-combustion and oxyfuel methods are still in development phase.
  • solvent-based PCC may be the most accessible option for retrofitting existing power plants.
  • Figure 2 shows a schematic of a solvent-based PCC process.
  • the flue gas passes through the absorber column (packed or tray) where the lean solvent enters from the top of the absorber in a countercurrent process.
  • the solvent removes CO2 from the flue gas through exothermic physico-chemical interaction; the rich solvent then exits from the absorber bottom, with higher temperature, while the cleaned flue gas leaves absorber overheads towards stack.
  • the stripper column the rich solvent is stripped of CO2 via thermal treatment.
  • the lean solvent is recycled to absorber while CO 2 is sent from overhead to a compression unit.
  • the energy for solvent regeneration of the PCC process is typically supplied by bleeding steam from power plant steam cycle. Furthermore, the PCC needs electricity for its auxiliary equipments including liquid pumps and CO 2 compressors. The overall energy penalty is estimated to be above 20%. This results in serious reduction in power plant efficiency.
  • the present invention seeks to provide a method of solvent regeneration which is more energy efficient and which thereby provides a post-combustion carbon capture process with a significantly reduced energy penalty than current processes.
  • a method of removing at least part of the carbon dioxide from a flue gas including the following steps:
  • step b heating the carbon dioxide rich liquid solvent in a vessel to separate carbon dioxide gas from the liquid solvent thereby providing a regenerated liquid solvent and a gas stream of carbon dioxide, wherein heating the carbon dioxide rich liquid solvent in step b is provided by heating the vessel via radiative heat transfer of solar energy.
  • a method of regenerating a carbon dioxide rich liquid solvent wherein the method includes heating the carbon dioxide rich liquid solvent in a vessel to separate carbon dioxide gas from the liquid solvent wherein heating the carbon dioxide rich liquid solvent is provided by heating the vessel via radiative heat transfer of solar energy.
  • the carbon dioxide rich liquid solvent is heated in step b. by the body of the vessel which in turn is heated via radiative heat transfer of solar energy.
  • the radiative heat transfer of solar energy is provided by an array of solar energy collectors.
  • a method of removing at least part of the carbon dioxide from a flue gas including the following steps:
  • heating the carbon dioxide rich liquid solvent in step b is provided by contacting the carbon dioxide rich liquid solvent with a condensing end of a heat pipe wherein heat is transferred to the heat pipe via radiative heat transfer of solar energy.
  • a method of regenerating a carbon dioxide rich liquid solvent wherein the method includes heating the carbon dioxide rich liquid solvent in a vessel to separate carbon dioxide gas from the liquid solvent wherein wherein heating the carbon dioxide rich liquid solvent in step b is provided by contacting the W
  • the vessel is in the form of a pipe or conduit.
  • the regenerated liquid solvent passes through a knock out drum where gaseous carbon dioxide is removed from the regenerated solvent.
  • FIG. 1 is a Schematic of CO 2 emitting process with Post Carbon Capture (PCC) facility
  • Figure 2 is a Schematic of a solvent-based PCC Process
  • Figure 3 is a Schematic of desorber with a kettle reboiler
  • Figure 4 is a Schematic of a coal-fired power plant with retrofitted PCC
  • Figure 5 is a Schematic of some options for fossil fuel-based repowering of power plants integrated with solvent-based PCC processes
  • Figure 6 is a Schematic of some options for renewable energy based repowering of power plants integrated with solvent-based PCC processes; repowering with a) solar energy, and b) wind energy;
  • Figure 7 is a Schematic of a coal-fired power plant with PCC while sourcing the reboiler energy from steam cycle and solar thermal energy;
  • Figure 8 is switching scheme for flexible operation of power plant
  • Figure 9 is a Schematic of an evacuated tube collector (heat pipe) as an example of a solar collector
  • Figure 10 is a structure of the heat transfer based on the available methodologies.
  • Figure 11 is a schematic of the heat transfer arrangement to the carbon dioxide rich solvent to produce the regenerated solvent in accordance with an embodiment
  • Figure 12 is a Schematic process diagram of a PCC process where the carbon dioxide rich solvent is regenerated by direct solar energy in accordance with one embodiment
  • Figure 13 is a Schematic of a coal-fired power plant with retrofitted PCC process in accordance with embodiment of Figure 12 ;
  • Figure 14 is a Schematic of a solar-assisted PCC in accordance with one embodiment with storage during a) day (sun available), b) night (sun unavailable). Grey color indicates the process inactivity.
  • Figure 15 is a Relation between solar fraction and a) solar collector area; b) annual economic benefit
  • Figure 16 is the relationship between solar collector area and carbon capture capacity
  • Figure 17 is the Economic comparison of conventional methodology and the current invention.
  • the word “comprising” means “including principally but not necessarily solely” or “having” or “including”, and not “consisting only of. Variations of the word “comprising”, such as “comprise” and “comprises” have correspondingly varied meanings.
  • FIGS 2 and 3 there is shown a typical solvent-based Post Carbon Capture (PCC) process 100 wherein the objective of the desorber 10 (also referred to in the art as a stripper) is to heat the liquid solvent rich in carbon dioxide in order to force the reverse kinetics to release the carbon dioxide. In cases when the saturation temperature of solvent and solute are very different then part of the solvent mixture can be evaporated to provide the stripping fluid.
  • PCC Post Carbon Capture
  • MEA has a saturation temperature of 170.4°C at atmospheric pressure, which is quite remote from that of water, being 100°C. Therefore, part of the liquid reaching the bottom of the desorber column 10 can be heated (reboiled) to a certain temperature to generate steam (see Figure 3). Further to this the recycled liquid from the condenser 5 can also be used for steam generation (see Figure 2). Therefore the key issues in desorber 10 design are reboiler pressure, reboiler temperature, and gas (steam) flowrate in the desorber column 10.
  • Reboiler 6 pressure and temperature are among the most critical (if not the main) parameters in desorber 10 design.
  • the reboiler 6 pressure should be enough to compensate for the pressure drop of the packed column and allow the gas phase (steam) to move up.
  • the reboiler 6 temperature is more complex than the pressure.
  • a higher desorber 10 (reboiler) temperature will expedite the regeneration process.
  • T 0 ** degradation temperature
  • the reboiler 6 temperature constraint can be written as T Reb ⁇ mm (V a '(P) (1) where V'(P) is obtained from flash vapor-liquid equilibrium calculations at pressure P.
  • the flowrate of the gas stream is another issue, Certainly, the objective is to use just enough steam to achieve the regeneration objective, as any extra steam will just add to the operating costs.
  • the exit gas from the top of the desorber 10 will contain mainly the target gas (CO 2 ) and steam.
  • the partial pressure of the target gas (TG) should be less than the equilibrium partial pressure of the inlet liquid [ ⁇ co,), ⁇ ⁇ Pco 2 @ « - «i? »t ] otherwise, reverse mass flow will occur, meaning that instead of desorbing the carbon dioxide from the liquid, more will be absorbed.
  • the flow rate of steam at the bottom of the reboiler should be such that at the top of column the partial pressure of steam becomes greater than pco * ' .
  • the temperature of the gas at the top of the column should be higher than the inlet liquid temperature (3 ⁇ 4t ⁇ ioLr) ⁇ to allow regeneration to initiate from the column top. It is therefore necessary that before desorber 10 modeling the reboiler temperature is decided and fed into the program.
  • the liquid temperature at the bottom of the column can also be set a few degrees below the reboiler 6 temperature tffur - ljw - AT).
  • Figure 4 illustrates the schematics of a power plant 150 retrofitted with a PCC unit 100.
  • the flue gas passes through the absorber column 9, interacts with MEA solvent and loses its carbon dioxide content before going to stack.
  • the steam required for the reboiler 6, can be extracted from IP or LP turbines. Therefore, the extracted steam and flue gas streams are the significant connections between power plant 150and the PCC unit 100.
  • Table 1 lists the results for integration of the base case 300 MWe coal-fired power plant with a PCC process.
  • PCC auxiliary compressors, flue gas blower, solvent pumps, etc.
  • MWe 17.2 net power output
  • MWe 17.2 net power output
  • MWe 227.9 gross electrical efficiency 0.28 net electrical efficiency 0.24 net efficiency reduction due to PCC (%) 19.4
  • the steam extraction 17 for solvent regeneration in the desorber column 10 is the main contributor for power plant load reduction (Figure 5a).
  • Numerous approaches have been proposed for integrated operation of power plant and PCC process while satisfying the maximum benefit of the market demand of electricity.
  • One of the early attempts has been repowering which can happen in either of two ways; one way is the installation of a small boiler 18 to generate the regeneration energy without the need for steam extraction from power plant steam cycle ( Figure 5b).
  • the other way is to extract regeneration energy from power plant steam cycle, but install a small natural gas turbine 19 to generate enough electricity to prevent load reduction (Figure 5c).
  • Solar thermal collectors 23 are devices designed to collect and convert the electromagnetic solar irradiation energy into more usable or storable energy form. They are usually categorized into two groups of non-concentrating and concentrating where for the former the collector area and absorber area are the same while they are different for the latter. The concentrating systems are costly and are usually used for generating high temperature steam from where electricity is generated. The non-concentrating collectors are less costly and are usually used for low-medium temperature fluid heating.
  • FIG. 7 illustrates a coal- fired power plant integrated with solvent based PCC process 100 and a system which makes use of solar energy 20.
  • SPCC solar-assisted PCC
  • the viability of such solar-assisted PCC (SPCC) 101 is location specific. It depends on environmental conditions (solar irradiance), cost of electricity, land availability, etc, Regions with high insolation, long summers, air- conditioning demand, and a reliance on coal-fired power plants would be the most promising candidates for the implementation of an SPCC system. This is not only because of the availability of solar resource but also because of the correlation between high electricity demand with solar irradiance.
  • the solvent may be regenerated to a lean solvent which may then be sent for use in the absorber of the post-combustion carbon capture process.
  • Figure 9 shows schematic of an evacuated tube collector (also referred to as a heat pipe) in which the solar energy 20 is transferred to a liquid inside the evacuated tube.
  • the liquid heats and moves to the tube condenser head 32 composed of copper.
  • the heat is then directly transferred to the working fluid 33 passing through the head of the tube 32 and heats it.
  • the working fluid 33 passed through the head of the tube 32 may be the carbon dioxide rich solvent and the heat directly transferred from the solar energy reflecting onto the evacuated tube collector is used to directly regenerate the solvent passing through as the working fluid.
  • the tube condenser head 32 protrudes into the pipe, or vessel, through which the carbon dioxide rich solvent 33 is passing which provides a better heat transfer via conductive heat transfer.
  • the ultimate goal of desorber 10 is to heat the rich solvent to break the C0 2 -solvent reaction bonds and separate them followed by sending C0 2 to storage and lean solvent to the absorber 9.
  • the overall heat transfer structure to the rich solvent in Figure 10, it is evident that the heat transfer from sun to the solvent passes through numerous stages (A - Heating Working Fluid Stage, B - Generation of Steam, C - Heating for steam of Reboiler, and D - The steam mixes with the rich solvent and passes its latent heat to the solvent for reverse reaction and breaking bonds) and each stage is subject to energy loss, which is compounded by the equipments and CAPEX required for each heat transfer stage.
  • the rich solvent 51 may be directly sent to the solar collector 23 where the heat transferred breaks the carbon dioxide solvent bonds of the carbon dioxide rich solvent 51 and changes the solvent to a regenerated solvent, or lean solvent, 52, without sending the solvent to a desorber 10.
  • the analogical heat, transfer structure of Figure 10 in the current methodology is illustrated in Figure 11. It is clear that such an arrangement has a significant advantage in the extent of the reduction of both the capital expenditure and operating expenditure of a typical PCC process 100.
  • the schematic solvent-based PCC process in accordance with an aspect of the present invention is shown in Figure 12. It is evident from the figure that the desorber column 10 along with the C0 2 condenser 5 and reboiler 6 are removed from the process flow diagram altogether.
  • flue gas 57 including carbon dioxide is introduced to an absorber 9 which removes at least some of the carbon dioxide from the flue gas by directly contacting and absorbing the carbon dioxide with a liquid solvent such as MEA.
  • the flue gas which has had carbon dioxide removed can exit at the top of the absorber column 9 via exhaust gas 58 which would be normally sent to a stack.
  • the solvent rich in carbon dioxide exits the bottom of the absorber and is sent via a heat exchanger 56 to a solar thermal collector 23 which receives solar radiation from the sun and provides heat to the carbon dioxide rich solvent 51 via radiative heat transfer which breaks the carbon dioxide solvent bonds of the carbon dioxide rich solvent 51 and changes the solvent to a regenerated solvent, or lean solvent, 52.
  • the lean solvent 52 exits the solar thermal collector 52 which includes carbon dioxide which is then removed from the stream 52 by a knock out drum 55 which sends the regenerated solvent from the bottom stream of the knock out drum 55 back to the absorber via heat exchanger 56 and releases the separated carbon dioxide from the top of the knock out drum 55.
  • the carbon dioxide may then be sent for compression, storage, further industrial use or sequestration as desired.
  • the integration of the power plant 150 and the proposed process in accordance with one embodiment is illustrated in Figure 13 and 14. In the integrated structure, two optional storage tanks 60, 61 (for lean 61 and rich solvent 60) are allocated for the conditions when the CO2 capture process 102 continues during the times when solar energy is unavailable.
  • the solar collection field 23 will be sized in such a capacity that it can provide enough energy for continuous solvent regeneration.
  • rich solvent from absorber 58 will be directed to rich solvent tank 60 and stored ( Figure 14b).
  • the solar field will regenerate both the stored rich solvent 67 and the rich solvent 57 coming directly from absorber ( Figure 14a).
  • the same amount of stored rich solvent 67 after regeneration will be stored in lean tank 61 for use during sun unavailability.
  • the present invention decouples the PCC system from power plants with eliminating the dependence of the PCC process on the power plant steam cycle. This reduces the operation complexity of power plant with carbon capture process.
  • the steam for the reboiler has to be bled from power plant steam cycle. This requires modification in the steam cycle and operation of the integrated process becomes complex.
  • the present invention does not require desorber column, CO2 condenser, and reboiler which is subject to notable reduction in capital costs in the range of 25- 30%.
  • the partial pressure of the C0 2 in the desorber column should be less than the equilibrium partial pressure of the inlet rich solvent. Otherwise, reverse mass transfer will occur, meaning that instead of desorbing the target component from the solvent, more CO 2 will be absorbed.
  • the flow rate of steam at the bottom of the reboiler should be high enough that at the top of column the partial pressure of steam becomes greater. This means that the energy of steam which is generated in the desorber column is much more than the energy required for solvent regeneration.
  • the reboiler energy is reported at best conditions around 3 MJ/kg-CC>2 and generally in the range of 3.5-5.0 MJ/kg-C0 2 .
  • the solvent receives the energy directly from sun without need to contact with steam. As such the energy duty will be quite close to its theoretical value (2.9 MJ/kg-CC ⁇ for the case-study discussed below).
  • the product CO2 stream will be combination of steam and C0 2 (with steam molar fraction being above 50%), notable cooling duty is required to cool the CC ⁇ -water stream and separate CO 2 .
  • the CO2 condenser is removed from the process and not required.
  • Example A 660 MWe coal-fired power plant is burning pulverized black coal and emitting 595 tonne/h of CO2.
  • the power plant aims to build a solvent-based PCC plant to capture 1.5 million tonnes of CO2 annually starting from year 2015.
  • the selected process is using 30 wt% Monoethanolamine MEA solvent with 90% C0 2 capture with product CO2 purity of 99%.
  • Such a plant will require 151.2 MWth energy for solvent regeneration which should be supplied by steam extraction from power plant steam cycle. This amount of thermal energy will reduce power load about 26.8 MWe.
  • the company has investigated the application of evacuated tube solar tliermal collectors for supplying part/whole of regeneration energy.
  • Figure 15a illustrates the relation between solar collector area and its fractional share of regenerator energy.
  • FIG 16 illustrates the area required for achieving the total solvent regeneration at various carbon capture rates. To capture of 1.5 million tonne of CO2 annually, area of 2.64x106 m 2 is required. Apart from the economic differences, such an area could only supply 84% of regeneration energy using conventional methodologies (Figure 15a).

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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 porte sur un procédé de régénération d'un solvant liquide riche en dioxyde de carbone, le procédé comprenant le chauffage du solvant liquide riche en dioxyde de carbone dans une cuve pour séparer du dioxyde de carbone gazeux du solvant liquide, le chauffage du solvant liquide riche en dioxyde de carbone étant assuré par chauffage de la cuve par transfert de chaleur par rayonnement à partir d'énergie solaire.
PCT/AU2014/000142 2013-02-19 2014-02-19 Procédé de régénération d'un absorbant pour la capture de dioxyde de carbone Ceased WO2014127410A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2013900549A AU2013900549A0 (en) 2013-02-19 A method of regenerating an absorbent for capture of carbon dioxide
AU2013900549 2013-02-19

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WO2014127410A1 true WO2014127410A1 (fr) 2014-08-28

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CN106999838A (zh) * 2014-10-23 2017-08-01 玻点太阳能有限公司 使用太阳能的气体净化和相关系统及方法
US9890183B2 (en) 2015-12-08 2018-02-13 General Electric Company Aminosilicone solvent recovery methods and systems
WO2021001673A1 (fr) 2019-07-02 2021-01-07 Total Se Extraction d'hydrocarbures à l'aide d'énergie solaire
CN114452779A (zh) * 2022-03-09 2022-05-10 清华大学 基于相变吸收剂的二氧化碳捕集系统
WO2023122475A1 (fr) * 2021-12-20 2023-06-29 General Electric Company Système et procédé pour réguler une température dans un absorbeur
WO2024017932A1 (fr) * 2022-07-21 2024-01-25 Shell Internationale Research Maatschappij B.V. Procédé de capture de co2 à partir d'air
US20250243806A1 (en) * 2024-01-30 2025-07-31 Ge Infrastructure Technology Llc Systems and methods for integrating auxiliary energy and waste heat recovery from gas turbine engines
WO2025189096A1 (fr) * 2024-03-08 2025-09-12 Schlumberger Technology Corporation Système et procédé destinés à fournir de l'énergie à une installation de captage de carbone

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CN201140032Y (zh) * 2007-11-16 2008-10-29 清华大学 利用太阳能脱除烟气中二氧化碳的装置
US20120192564A1 (en) * 2011-01-31 2012-08-02 Hitachi, Ltd. Thermal Power Plant with Carbon Dioxide Capture Scrubbing Equipment
WO2012173855A2 (fr) * 2011-06-10 2012-12-20 Joule Unlimited Technologies, Inc. Systèmes et procédés de distribution de dioxyde de carbone, systèmes de bioréacteurs et leurs utilisations

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CN201140032Y (zh) * 2007-11-16 2008-10-29 清华大学 利用太阳能脱除烟气中二氧化碳的装置
US20120192564A1 (en) * 2011-01-31 2012-08-02 Hitachi, Ltd. Thermal Power Plant with Carbon Dioxide Capture Scrubbing Equipment
WO2012173855A2 (fr) * 2011-06-10 2012-12-20 Joule Unlimited Technologies, Inc. Systèmes et procédés de distribution de dioxyde de carbone, systèmes de bioréacteurs et leurs utilisations

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106999838A (zh) * 2014-10-23 2017-08-01 玻点太阳能有限公司 使用太阳能的气体净化和相关系统及方法
EP3185991A4 (fr) * 2014-10-23 2018-04-25 Glasspoint Solar, Inc. Purification de gaz au moyen de l'énergie solaire, ainsi que systèmes et procédés associés
US10065147B2 (en) 2014-10-23 2018-09-04 Glasspoint Solar, Inc. Gas purification using solar energy, and associated systems and methods
US9890183B2 (en) 2015-12-08 2018-02-13 General Electric Company Aminosilicone solvent recovery methods and systems
WO2021001673A1 (fr) 2019-07-02 2021-01-07 Total Se Extraction d'hydrocarbures à l'aide d'énergie solaire
US11859477B2 (en) 2019-07-02 2024-01-02 Totalenergies Se Hydrocarbon extraction using solar energy
WO2023122475A1 (fr) * 2021-12-20 2023-06-29 General Electric Company Système et procédé pour réguler une température dans un absorbeur
US12318727B2 (en) 2021-12-20 2025-06-03 Ge Infrastructure Technology Llc System and method for controlling a temperature in an absorber
CN114452779A (zh) * 2022-03-09 2022-05-10 清华大学 基于相变吸收剂的二氧化碳捕集系统
WO2024017932A1 (fr) * 2022-07-21 2024-01-25 Shell Internationale Research Maatschappij B.V. Procédé de capture de co2 à partir d'air
US20250243806A1 (en) * 2024-01-30 2025-07-31 Ge Infrastructure Technology Llc Systems and methods for integrating auxiliary energy and waste heat recovery from gas turbine engines
US12480444B2 (en) * 2024-01-30 2025-11-25 Ge Infrastructure Technology Llc Systems and methods for integrating auxiliary energy and waste heat recovery from gas turbine engines
WO2025189096A1 (fr) * 2024-03-08 2025-09-12 Schlumberger Technology Corporation Système et procédé destinés à fournir de l'énergie à une installation de captage de carbone

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