WO2014175478A1 - Appareillage pour séparer et collecter le co2 comportant un appareil de désoxydation - Google Patents

Appareillage pour séparer et collecter le co2 comportant un appareil de désoxydation Download PDF

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Publication number
WO2014175478A1
WO2014175478A1 PCT/KR2013/003516 KR2013003516W WO2014175478A1 WO 2014175478 A1 WO2014175478 A1 WO 2014175478A1 KR 2013003516 W KR2013003516 W KR 2013003516W WO 2014175478 A1 WO2014175478 A1 WO 2014175478A1
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Prior art keywords
flue gas
carbon dioxide
absorbent
oxygen
amine
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Ceased
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PCT/KR2013/003516
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English (en)
Korean (ko)
Inventor
백일현
박기태
유정균
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Korea Institute of Energy Research KIER
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Korea Institute of Energy Research KIER
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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
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • 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
    • 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
    • B01D53/1431—Pretreatment by other processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/869—Multiple step processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/104—Oxygen
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/32—Direct CO2 mitigation

Definitions

  • the present invention relates to a carbon dioxide separation and recovery apparatus having a oxygen removal device capable of preventing deterioration of the absorbent by removing residual oxygen contained in the flue gas before entering the absorption tower for carbon dioxide separation recovery and its process method It is about.
  • Carbon Dioxide Capture & Storage (CCS) technology is a technology that isolates carbon dioxide from the atmosphere from carbon dioxide sources such as power plants, steel and cement plants due to the use of fossil fuels.
  • carbon dioxide capture technology is a core technology that accounts for 70 to 80% of the total cost.
  • Postcombustion technology, pre-combustion technology, and oxy-oxygen combustion technology (Oxy) I fuel combustion technology) (the latest development status of carbon dioxide capture technology Chang-Keun Lee, Industrial Chemistry Prospect, Vol. 12, No. 1, 2009).
  • Postcombustion technology is a technique for absorbing or reacting carbon dioxide (C0 2 ) from fossil fuel combustion in various solvents and precombustion technology is used for combustion.
  • the separation of carbon dioxide before is carried out by gasifying fossil fuels such as coal to convert it to C0 2 and hydrogen, and then to separate carbon dioxide (C0 2 ) from carbon dioxide (C0 2 ) / hydrogen () mixed gas.
  • It is a technique for easily capturing carbon dioxide (C0 2 ) in exhaust gas by combusting or burning a mixed gas.
  • Oxy-fuel combustion technology is a technology that facilitates the capture of carbon dioxide (C0 2 ) by burning only using oxygen instead of air when burning fossil fuel. Post-combustion capture is the most widely used of the above techniques.
  • Post combustion capture technology which captures carbon dioxide contained in flue gas after combustion, uses a method of absorbing, regenerating, and separating carbon dioxide using an absorbent.
  • the main research directions are focused on improvement of absorbent performance and process improvement.
  • This technology is already operating wet absorption technology and dry adsorption technology to supply carbon dioxide necessary for urea fertilizer production, automatic welding, carbonated drinks, etc., and the efficiency of wet absorption technology is high.
  • the representative process of the wet absorption technology is a capture process using an amine-based absorbent, which is a technology that has secured the technical reliability applied in the reforming process of the petrochemical process, but it is applied to the flue gas which is a combustion flue gas containing various pollutants.
  • Application requires improvements in absorbent performance and process.
  • the process using an amine-based absorbent is a chemical absorption process using an alkanolamine in which an amine and a hydroxyl group are bonded to an alkyl group as an absorbent to regenerate an absorption tower that selectively absorbs carbon dioxide from an inlet gas and an absorber that absorbs carbon dioxide. It is composed of stripping tower (heating regeneration tower) and auxiliary equipment.
  • Mono ethanol amine the most widely used amine absorbent, provides the cause of acidic carbon dioxide and acid-base neutralization reactions in alkaline aqueous solutions formed by unshared electrons of amine groups. (carbamate or bicarbonate) is decomposed and regenerated at about 110 to 130 ° C.
  • the amine absorbent may include DEA (diethanol amine), TEA (tr iethanolamine), MDEA (methyldi ethanol amine), DIPA (di iso-propanolamine) and AMP (2-amino-2-methyl-l-propanol). Idol has a lot of difference in absorption capacity and absorption rate of carbon dioxide according to the structural characteristics.
  • Ethylenedi amine tetraacet icacid, etc. is used.
  • other additives must be used, but additives added to prevent deterioration may incur additional operating costs and induce side effects in the entire absorption process.
  • a process of removing oxygen (Korean Patent 1038674) before absorbing carbon dioxide and the like before reaching a stripping column that undergoes a heat regeneration process has also been attempted.
  • oxidative degradation occurs already. Therefore, it is necessary to fundamentally block the absorbent deterioration by blocking the absorbent and oxygen beforehand.
  • a process of removing oxygen contained in the flue gas before reaching the absorption tower is performed so that oxygen is not absorbed simultaneously when carbon dioxide (C0 2 ) is absorbed by the amine-based absorbent in the absorption tower.
  • flue gas is the selective catalytic reduction
  • the present inventors Before reaching the (SCR) device, the present inventors have found that the oxygen elimination effect can be maximized by passing a catalytic combustor which removes oxygen through catalytic combustion in flue gas containing carbon dioxide and oxygen, thereby completing the present invention. .
  • the present invention provides a catalytic combustor for removing oxygen through catalytic combustion in a flue gas containing carbon dioxide and oxygen;
  • An optional catalytic reduction (SCR) device for removing NOx of flue gas that has passed through the catalytic combustor;
  • An electrostatic precipitator (EP) for removing dust of the flue gas passing through the selective catalytic reduction device;
  • Flue gas desulfurization to remove SOx of flue gas passed through the electrostatic precipitator (EP) FGD: Flue gas desulfuriation
  • a temperature dropping device for lowering the temperature of the flue gas passing through the flue gas desulfurization device (DCC: Direct Contacting Cooler);
  • DCC Direct Contacting Cooler
  • the flue gas and the amine-based absorber passed through the temperature lowering device is supplied, the supplied amine-based absorber absorbs carbon dioxide contained in the exhaust gas to produce a saturated carbon dioxide absorbent, the gas component unreacted with the amine-based absorber Absorption tower to discharge the
  • the catalyst in the catalytic burner is platinum (Pt), rhodium (Rh), palladium
  • a carbon dioxide separation and recovery apparatus having an oxygen removal apparatus using an oxidation catalyst selected from the group consisting of (Pd).
  • the present invention also provides a catalytic combustor, at least one selected from the group consisting of methane, ethane propane, butane, pentane nucleus, heptane, octane, nonane, decane, undecane, and dodecane as hydrocarbons.
  • a catalytic combustor at least one selected from the group consisting of methane, ethane propane, butane, pentane nucleus, heptane, octane, nonane, decane, undecane, and dodecane as hydrocarbons.
  • a carbon dioxide separation recovery device having an oxygen removal device.
  • the present invention also provides a carbon dioxide separation and recovery apparatus having an oxygen removal device using a regeneration method of directly heating and engraving a ceramic having a large surface area.
  • the present invention also provides a catalytic combustion apparatus comprising an SCR reactor activated by flue gas introduced into the reactor without reheating, and a reducing agent supply line for supplying NH 3 into the SCR reactor, wherein the activation temperature of the catalyst is Provided is a carbon dioxide separation recovery device having an oxygen removal device, which is set at 320 ° C.
  • the flue gas desulfurization apparatus uses a wet method, and absorbs so 2 in the gaseous phase by using an absorbent of water or an alkaline solution to dehydrate the alkaline components, reactions, and sludge produced.
  • a carbon dioxide separation rare water device having an oxygen removal device.
  • the present invention also provides a carbon dioxide separation and recovery apparatus having an oxygen removal device, wherein the temperature dropping device lowers the temperature of the flue gas discharged from the flue gas desulfurization device to 40 to 45 ° C. do.
  • the present invention also provides a carbon dioxide separation and recovery apparatus having an oxygen removal device using an amine absorbent used in the absorption tower.
  • the present invention also provides the amine absorbent is MEA (Monoethanol amine),
  • a carbon dioxide separation recovery device having an oxygen removal device, which is at least one selected.
  • the carbon dioxide separation and recovery apparatus including the oxygen removing device and the process method thereof according to the present invention remove dissolved oxygen in the flue gas through a catalytic combustion device. Accordingly, the dissolved oxygen is removed before the flue gas reaches the absorption tower to prevent oxidation of the absorbent and to solve the degradation caused by the oxidation.
  • FIG. 1 is a process conceptual diagram showing a carbon dioxide separation recovery process provided with an oxygen removing device of the present invention.
  • FIG. 2 is a conceptual diagram showing a catalytic combustion reaction.
  • FIG. 1 is a process conceptual diagram illustrating a carbon dioxide separation recovery process including an oxygen removing device.
  • the carbon dioxide separation and recovery apparatus including the oxygen removal device includes a combustor (1), a catalytic combustion device (2), a selective reduction catalyst device (3), an electrostatic precipitator (4), a flue gas desulfurization device (5), and The descent apparatus 6, the absorption tower 7, and the stripping tower 8.
  • the combustor 1 is combusted by injecting fossil fuels such as liquefied petroleum gas (LPG), liquefied natural gas (LNG), petroleum and coal and air containing excess oxygen to burn the combustion.
  • fossil fuels such as liquefied petroleum gas (LPG), liquefied natural gas (LNG), petroleum and coal and air containing excess oxygen to burn the combustion.
  • LPG liquefied petroleum gas
  • LNG liquefied natural gas
  • CO carbon monoxide
  • HC unburned carbon
  • fly ash which is a dust generated when incineration of coal dust as coal as a raw material of about 1,400 to l, 50 (rc), is directly discharged from the combustor.
  • the flue gas from which the fly ash is removed includes 0 2 , N 2 , which does not participate in the combustion reaction, and combustion byproducts C0 2 , N0 2 , NO, NOx, SOx, CO, HC, and the like. Is discharged and fed to the catalytic combustion device (2).
  • the catalytic combustion apparatus 2 performs a process of reacting incomplete combustion gas such as CO and NO with residual oxygen.
  • a combustion agent may be further injected into the catalytic combustor to remove residual oxygen.
  • hydrocarbons such as methane, ethane, propane, butane, pentane, nuclear coal, heptane, octane, nonane, decane, undecane, dodecane, and the like are injected into the combustor.
  • the selective catalytic reduction apparatus 3 removes NOx remaining in the flue gas.
  • the selective catalytic reduction apparatus 3 selectively reduces NOx in flue gas to nitrogen and water vapor by ammonia reaction while simultaneously passing flue gas and ammonia (NH 3 ) reducing agent in the catalyst layer.
  • the reaction scheme is as follows.
  • the catalyst is a flue gas supplied inside without reheating.
  • SCR reactor activated by the, and a reducing agent supply line for supplying N3 ⁇ 4 into the SCR reactor, the activation temperature of the catalyst is set to less than 320 ° C.
  • the dust contained in the flue gas from which NOx has been removed through the selective reduction catalyst device 3 is removed through the electrostatic precipitator 4.
  • the electrostatic precipitator 4 separates the dust in the flue gas by moving it to the wall surface of the apparatus by using an electrostatic force.
  • Flue gas from which dust has been removed through the electrostatic precipitator 4 is supplied to the flue gas desulfurization apparatus 5.
  • the flue gas desulfurization apparatus 5 removes SOx contained in the exhaust gas after combustion by using the principles of absorption, adsorption, oxidation, reduction, and the like.
  • the flue gas desulfurization apparatus (5) uses a wet method, and absorbs SO 2 in the gaseous phase by using an absorbent of water or an alkaline solution to dehydrate the alkaline components, reactions and fish sludge. It is a device for treatment and disposal or for the production of marketable by-products such as gypsum.
  • the flue gas from which SOx is removed is supplied to the silver degassing apparatus.
  • the temperature drop device lowers the temperature so that the carbon dioxide contained in the flue gas can be absorbed by the amine-based absorbent.
  • the silver lowering device 6 is to drop the temperature of the flue gas of 55 to 60 ° C from which the SOx discharged from the flue gas desulfurization apparatus 5 is removed to 40 to 45 ° C. give.
  • the temperature reduced flue gas and the absorbent are supplied to the absorption tower (7).
  • the absorbent supplied absorbs carbon dioxide contained in the mixed gas to produce a saturated carbon dioxide absorbent, and discharges the absorbent and uncoated gas components.
  • the absorbent used in the absorption tower 7 uses an amine heat absorber, and the absorbent is ME Monoethanol amine, DGA (Diglycolamine), MDEA (N-Me t hy). At least one selected from the group consisting of 1 diet hano 1 am i ne), DEACDiethanol amine), Triethanolamine (TEA), AMP (2—Amino 2—methyl 1-propanol), and PZ (Piperazine), DIPA (Diisopropanolamine) Use.
  • ME Monoethanol amine DGA (Diglycolamine), MDEA (N-Me t hy). At least one selected from the group consisting of 1 diet hano 1 am i ne), DEACDiethanol amine), Triethanolamine (TEA), AMP (2—Amino 2—methyl 1-propanol), and PZ (Piperazine), DIPA (Diisopropanolamine) Use.
  • the carbon dioxide saturated absorbent removed by discharging the gas component unreacted with the absorbent is preheated through a heat exchanger and then supplied to the stripping column 8.
  • the carbon dioxide supplied to the stripping column (8) is caused by the saturated energy absorbed by the thermal energy generated by the reboiler below the stripping column.
  • the carbon dioxide is stripped off and the absorbent is regenerated and fed back to the absorption tower (7).
  • FIG. 2 is a conceptual diagram showing a reaction of a catalytic combustion device.
  • the catalytic combustion device 2 uses a regeneration method of directly heating and cooling a ceramic having a large surface area.
  • the catalytic combustion device 2 After forcibly supplying flue gas discharged from the combustor 1 into the catalytic combustion device 2 using a press-fit blower (not shown), the catalytic combustion device 2 The flue gas supplied inside is preheated to a temperature close to the combustion chamber temperature by the heat storage material 30 at the inlet side of the catalytic combustion device 2. The preheated flue gas is oxidized and decomposed in a completely burned silver 750 to 80 CTC by an auxiliary burner 10 in the combustion chamber and treated as a harmless and odorless gas. The treated flue gas passes through the heat storage material 50 on the outlet side, and heats waste heat of high temperature to the heat storage material and is sensed to a predetermined temperature, and then enters the selective reduction catalyst device 3 through the exhaust pipe 40.
  • the catalyst 20 used in the catalytic combustion device 2 is used by supporting platinum (Pt), rhodium (Rd) and palladium (Pd).
  • Pt platinum
  • Rd rhodium
  • Pd palladium
  • metals of platinum and palladium are used as a catalyst for converting carbon monoxide (CO) into carbon dioxide (C0 2 ) and hydrocarbons (HC) into carbon dioxide (C0 2 ) and water (3 ⁇ 40).
  • Rhodium is NO (NOx)
  • the heat storage material is to use the waste heat of the flue gas as much as possible, and to use it for preheating the flue gas, and to maximize the recovery of the waste heat, without using a heat exchanger, a ceramic having a large surface area Direct heating and cooling heat storage
  • Combustor Catalytic combustion device

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention porte sur un procédé pour éliminer l'oxygène contenu dans un gaz de carneau avant que le gaz de carneau n'atteigne une tour d'absorption de telle sorte que l'oxygène ne soit pas absorbé simultanément quand le CO2 est absorbé par un absorbant à base d'amine dans la tour d'absorption, de façon à résoudre un phénomène de dégradation de l'absorbant du CO2. L'appareillage de séparation et de collecte du CO2 et le procédé de traitement selon la présente invention éliminent l'oxygène dissous se trouvant dans un gaz de carneau grâce à un appareil de combustion catalytique. En conséquence, l'oxygène dissous est éliminé avant que le gaz de carneau n'atteigne la tour d'absorption, ce qui empêche l'effet oxydatif d'un absorbant et résout le phénomène de dégradation provoqué par l'effet oxydatif.
PCT/KR2013/003516 2013-04-24 2013-04-24 Appareillage pour séparer et collecter le co2 comportant un appareil de désoxydation Ceased WO2014175478A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2013-0045283 2013-04-24
KR20130045283A KR101485952B1 (ko) 2013-04-24 2013-04-24 산소제거 장치를 구비한 이산화탄소 분리 회수 장치

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Cited By (3)

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WO2016155929A1 (fr) * 2015-04-02 2016-10-06 Siemens Aktiengesellschaft Dispositif et procédé de séparation de dioxyde de carbone d'un flux gazeux
US20220314161A1 (en) * 2021-04-02 2022-10-06 Kabushiki Kaisha Toshiba Gas processing equipment and gas processing method, and carbon dioxide capture system and carbon dioxide capture method
CN119490165A (zh) * 2023-08-18 2025-02-21 中国石油化工股份有限公司 一种用烟气同时制取二氧化碳和氮气的方法

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KR102248613B1 (ko) * 2019-07-29 2021-05-07 한국과학기술연구원 아민계 이산화탄소 흡착제용 금속산화물 촉매, 이를 포함하는 아민계 이산화탄소 흡착제 및 흡탈착 장치

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