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WO2025162151A1 - 捕集后脱碳气体的回收方法、系统及活性炭浓缩装置 - Google Patents

捕集后脱碳气体的回收方法、系统及活性炭浓缩装置

Info

Publication number
WO2025162151A1
WO2025162151A1 PCT/CN2025/074093 CN2025074093W WO2025162151A1 WO 2025162151 A1 WO2025162151 A1 WO 2025162151A1 CN 2025074093 W CN2025074093 W CN 2025074093W WO 2025162151 A1 WO2025162151 A1 WO 2025162151A1
Authority
WO
WIPO (PCT)
Prior art keywords
activated carbon
gas
compartment
decarbonized
steam
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/CN2025/074093
Other languages
English (en)
French (fr)
Inventor
鄞铃
郭东方
张庆文
李野
朱磊
王焕君
刘练波
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.)
Shanghai Shidongkou No2 Power Plant Huaneng International Power Co Ltd
Huaneng Clean Energy Research Institute
Original Assignee
Shanghai Shidongkou No2 Power Plant Huaneng International Power Co Ltd
Huaneng Clean Energy Research Institute
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 Shanghai Shidongkou No2 Power Plant Huaneng International Power Co Ltd, Huaneng Clean Energy Research Institute filed Critical Shanghai Shidongkou No2 Power Plant Huaneng International Power Co Ltd
Publication of WO2025162151A1 publication Critical patent/WO2025162151A1/zh
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • B01D53/1456—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
    • B01D53/02—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
    • 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • 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
    • B01D2252/20405—Monoamines
    • 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

Definitions

  • the present disclosure relates to the technical field of greenhouse gas emission reduction and resource utilization, and in particular to a method and system for recovering captured decarbonized gas and an activated carbon concentration device.
  • CO2 carbon dioxide
  • the power sector contributes significantly to CO2 emissions, accounting for 45% of the nation's total.
  • my country has developed a number of carbon reduction policies and targeted technical measures, such as pre-combustion capture, oxygen-enriched combustion, and post-combustion capture.
  • Post-combustion capture is one of the most mature technologies, with demonstration projects already established in hundreds of regions around the world and ongoing process improvements and optimization.
  • a common capture process uses an organic amine solution, highly selective for CO2, for absorption followed by heating and regeneration, producing high-purity CO2 for storage.
  • the flue gas after absorption by the organic solvent, is discharged through the top of the absorption tower.
  • the remaining gas components primarily include VOCs (volatile organic compounds), organic amines volatilized from the absorbent, a small amount of uncaptured CO2, and moisture.
  • the residual gas discharged contains not only harmful substances, but also recyclable organic amines, CO2 gas and water, etc. Directly discharging the residual gas into the atmosphere will not only waste resources, but also cause secondary pollution to the air.
  • the present disclosure provides a method and system for recovering decarbonized gas after capture, and an activated carbon concentration device to solve at least one of the above-mentioned problems.
  • an activated carbon concentration device for captured decarbonized gas, which recycles and processes the decarbonized gas output from a carbon capture absorption tower, and comprises: at least two compartments, each compartment containing activated carbon, and each compartment controlling the flow direction of the decarbonized gas through its own air intake valve; an activated carbon adsorption efficiency determination unit for determining the adsorption efficiency of the activated carbon in each compartment; and an air intake valve controller for controlling the air intake valve of the compartment to close and the air intake valve of another compartment to open when the adsorption efficiency of the activated carbon in the compartment is lower than a predetermined value, so that the activated carbon in the other compartment can adsorb the decarbonized gas.
  • each compartment inputs high-temperature steam into the reboiler through its own steam input valve.
  • the device also includes: a steam input valve controller, which is used to control the steam input valve of the compartment to open after the air inlet valve of the compartment is closed, so that the high-temperature steam of the reboiler can enter the compartment and desorb the gas adsorbed by the activated carbon in the compartment.
  • the device also includes: a reflux pipe for returning the desorbed gas to the desorption tower in the form of steam.
  • the device also includes: an air supply fan, a three-ventilation valve and a burner, wherein: after the air inlet valve of the cabin is closed, the remaining gas in the cabin after activated carbon adsorption is input into the burner through the air supply fan and the three-ventilation valve.
  • a recovery system for decarbonized gas after capture comprising: the above-mentioned activated carbon concentration device for decarbonized gas after capture, a carbon capture absorption tower, a reboiler and a desorption tower, wherein the desorption tower desorbs the carbon dioxide entering from the carbon capture absorption tower through the heating treatment of the reboiler.
  • the desorption tower recovers the desorption-treated gas output from the activated carbon concentration device and refluxed in the form of steam, and performs a temperature-raising operation based on the heat of the steam.
  • a method for recovering decarbonized gas after capture comprising: providing at least two chambers, each chamber containing activated carbon, wherein the chambers are connected to a carbon capture absorption tower, and the chambers control the flow direction of the decarbonized gas output from the carbon capture absorption tower through their own air intake valves; in response to the decarbonized gas entering the chamber, determining the adsorption efficiency of the activated carbon in the chamber; when the adsorption efficiency of the activated carbon in the chamber is lower than a predetermined value, controlling the air intake valve of the chamber to close and opening the air intake valve of another chamber to facilitate the activated carbon in the other chamber to adsorb the decarbonized gas.
  • each compartment inputs high-temperature steam into the reboiler through its own steam input valve; after the air inlet valve of the compartment is closed, the steam input valve of the compartment is controlled to open so that the high-temperature steam from the reboiler enters the compartment to desorb the gas adsorbed by the activated carbon in the compartment.
  • the method further comprises: returning the desorbed gas to the desorption tower in the form of steam.
  • the method further includes: pre-setting an air supply fan, a three-ventilation valve and a burner; after the air inlet valve of the cabin is closed, the remaining gas in the cabin after activated carbon adsorption is input into the burner through the air supply fan and the three-ventilation valve.
  • the present disclosure also provides a computer device, including a memory, a processor, and a computer program stored in the memory and executable on the processor, wherein the above method is implemented when the processor executes the computer program.
  • the present disclosure also provides a computer-readable storage medium, which stores a computer program for executing the above method.
  • this technical solution can realize the adsorption and desorption treatment of decarbonized gas by setting up a cabin containing activated carbon, thereby realizing the recycling of decarbonized gas, thereby reducing resource waste and reducing the probability of pollution.
  • FIG1 is a schematic diagram of a system for recovering captured decarbonized gas according to an embodiment of the present disclosure.
  • FIG2 is a structural block diagram of an activated carbon concentration device for capturing decarbonized gas according to an embodiment of the present disclosure.
  • FIG3 is a flow chart of a method for recovering captured decarbonized gas according to an embodiment of the present disclosure.
  • the residual gas (also known as decarbonized gas) discharged from the absorption tower contains not only harmful substances but also reusable organic amines, CO2 gas, and water. If the residual gas is directly discharged into the atmosphere, it will not only waste resources but also cause secondary air pollution.
  • the embodiment of the present disclosure provides a recovery scheme for the decarbonized gas after capture.
  • this scheme can recycle and reuse the gas components in the decarbonized gas, reduce resource waste, and reduce the probability of pollution; on the other hand, the heat recovered from the desorption steam can be used to heat the desorption tower, which can reduce the energy consumption of the reboiler.
  • FIG1 is a schematic diagram of a post-capture decarbonized gas recovery system according to an embodiment of the present disclosure.
  • the system includes a post-combustion capture device 13 and an activated carbon concentration device 14 for the post-capture decarbonized gas.
  • the activated carbon concentration device 14 recovers the decarbonized gas captured by the post-combustion capture device 13.
  • FIG2 is a block diagram of the structure of the activated carbon concentration device 14.
  • the activated carbon concentration device 14 includes: at least two compartments 7, an activated carbon adsorption efficiency determination unit 142 and an intake valve controller 143, wherein:
  • Each compartment contains activated carbon, which can absorb decarbonized gas.
  • Each compartment controls the flow direction of the decarbonized gas through its own air inlet valve.
  • the activated carbon adsorption efficiency determination unit 142 is used to determine the adsorption efficiency of the activated carbon in each compartment.
  • the activated carbon adsorption efficiency determination unit 142 can be two gas analyzers set at the inlet and outlet of the cabin, used to measure the concentration of gases (for example, CO and CO2) and determine the adsorption efficiency of the activated carbon in the cabin based on the concentration difference between the inlet and outlet gases.
  • gases for example, CO and CO2
  • the air intake valve controller 143 is used to control the air intake valve of the compartment to close and the air intake valve of another compartment to open when the adsorption efficiency of the activated carbon in the compartment is lower than a predetermined value (the predetermined value can be determined according to actual conditions and is not limited in the present disclosure), so that the activated carbon in the other compartment can adsorb the decarbonized gas.
  • each compartment can also receive high-temperature steam from the reboiler via its own steam input valve.
  • the activated carbon concentrator 14 further includes a steam input valve controller configured to control the opening of the steam input valve in a compartment after the compartment's air inlet valve is closed, thereby allowing the high-temperature steam from the reboiler to enter the compartment and desorb the gas adsorbed by the activated carbon in the compartment.
  • the activated carbon concentrator 14 also includes a reflux line for returning the desorbed gas to the desorption tower in the form of steam.
  • the desorbed gas primarily includes reusable organic amines and CO2. The desorption tower then recycles these gases.
  • the activated carbon concentrator 14 further includes an air supply blower, a three-way ventilation valve, and a burner. After the air inlet valve of the chamber is closed, the remaining gas in the chamber after activated carbon adsorption is fed into the burner through the air supply blower and the three-way ventilation valve. This remaining gas is clean air and can be fed into the burner for further use.
  • the post-combustion capture device 13 includes: a carbon capture absorption tower 1, a rich liquid pump 2, a lean and rich liquid heat exchanger 3, a lean liquid pump 4, a desorption tower 5 and a reboiler 6;
  • the activated carbon concentration device 14 includes: a cabin 7, an air intake control valve 8, a steam desorption control valve 9, an air supply fan 10, a three-ventilation valve 11 and a burner 12.
  • the desorption tower 5 desorbs carbon dioxide entering the carbon capture and absorption tower 1 through heating by the reboiler 6.
  • the decarbonized gas from the carbon capture and absorption tower 1 enters the activated carbon concentrator 14 for adsorption and desorption.
  • the desorption tower 5 recovers the desorbed gas, which is refluxed in the form of steam from the chamber 7 of the activated carbon concentrator 14, and heats the desorbed gas using the heat of the steam.
  • the gas components in the decarbonized gas can be recycled and reused, reducing resource waste and lowering the probability of pollution. Furthermore, the desorption tower 5 uses steam heat to increase the temperature, which can reduce the energy consumption of the reboiler.
  • the flue gas from the power plant undergoes desulfurization, denitrification and dust removal pretreatment and then enters the carbon capture absorption tower 1. It fully contacts the carbon capture solvent lean liquid from bottom to top.
  • the carbon dioxide in the flue gas is absorbed by the lean liquid (the lean liquid is produced by the lean liquid pump 4) and then falls to the bottom of the tower under the action of gravity.
  • the rich liquid pump 2 Under the power of the rich liquid pump 2, it enters the lean-rich liquid heat exchanger 3 for sufficient heat exchange with the hot lean liquid.
  • the solution enters the carbon dioxide desorption tower 5. Under the action of the reboiler 6, it is heated and the carbon dioxide and part of the water vapor are desorbed.
  • the decarbonized gas generated in the absorption tower 1 enters the cabin 7 of the activated carbon concentration device from the top of the absorption tower 1 through the air intake control valve 8 (which has the function of the above-mentioned air intake valve controller).
  • the porous structure and good adsorption performance of the activated carbon in the cabin absorb the incompletely absorbed carbon dioxide gas, carbon monoxide gas and other components in the decarbonized gas.
  • the adsorbed clean air is controlled by the air supply fan 10 and the three-way ventilation valve 11, with part of it being fed into the boiler burner 12 and part of it being discharged normally.
  • the aforementioned chamber 7 has a two- or multi-chamber structure.
  • the air inlet valve of one chamber When the air inlet valve of one chamber is open, that chamber performs flue gas adsorption. Subsequently, based on the gas analysis data at the chamber inlet and outlet, the concentrations of carbon monoxide (CO) and carbon dioxide (CO2) are measured to determine the activated carbon adsorption efficiency.
  • CO carbon monoxide
  • CO2 carbon dioxide
  • two gas analyzers can be installed at the inlet and outlet of chamber 7 to measure CO and CO2 concentrations. The difference in gas concentrations at the inlet and outlet can be used to determine the activated carbon adsorption efficiency within the chamber.
  • the air inlet valve of the compartment is closed, and the air inlet valve of the other compartment is opened to continue the gas adsorption work.
  • the remaining steam from the reboiler 6 is introduced into the compartment through the steam desorption control valve 9 via the insulation pipeline, and the gas components in the activated carbon pores are desorbed and regenerated with high-temperature steam.
  • the steam carrying carbon dioxide after stripping and the water liquid falling back to the bottom of the cabin enter the desorption tower 5 through the pipeline (i.e., the above-mentioned reflux pipe).
  • the air inlet valve of the other compartment is closed, and the air inlet valve of the compartment is opened, and the cycle is repeated to maintain the synchronous adsorption and desorption work of multiple compartments. In this way, the efficiency of decarbonized gas recovery and treatment can be improved.
  • the air intake valve and steam desorption control valve can be electric, and the valve switch can be manually controlled by the electric valve PLC (Programmable Logic Controller).
  • PLC Programmable Logic Controller
  • the activated carbon concentration device 14 can be set up with 2 to N compartments according to the actual scenario.
  • the gas flow direction between the multiple compartments is controlled by valves, and the multiple compartments work synchronously by adopting the method of partitioned adsorption and partitioned desorption. There is no risk of suspending the equipment operation for desorption, which can ensure work efficiency.
  • the disclosed embodiments replace the traditional water scrubber treatment process for decarbonized tail gas (i.e., decarbonized gas) with activated carbon adsorption and concentration, efficiently recovering and separating unabsorbed carbon dioxide, escaped organic amine absorbent, and water from the decarbonized tail gas, thereby reducing waste of effective resources and water and electricity consumption in the water scrubbing process. Furthermore, by utilizing the activated carbon's efficient capture of organic matter and absorbing other gaseous components in the tail gas, secondary air pollution caused by direct discharge can be prevented.
  • decarbonized tail gas i.e., decarbonized gas
  • activated carbon adsorption and concentration efficiently recovering and separating unabsorbed carbon dioxide, escaped organic amine absorbent, and water from the decarbonized tail gas, thereby reducing waste of effective resources and water and electricity consumption in the water scrubbing process. Furthermore, by utilizing the activated carbon's efficient capture of organic matter and absorbing other gaseous components in the tail gas, secondary air pollution caused by direct discharge can be prevented.
  • the embodiment of the present disclosure makes full use of the residual steam heat from steam regeneration after carbon dioxide capture to perform heated steam desorption and regeneration on the gas molecules adsorbed in the activated carbon pores, thereby restoring the adsorption performance of the activated carbon.
  • high-temperature steam is used to recover the CO2, organic amines and other components adsorbed in the pores in the form of steam and reflux them into the desorption tower. This will not generate excess waste liquid and reduce the cost of secondary treatment of wastewater and waste.
  • the embodiment of the present disclosure refluxes the desorbed liquid from the activated carbon concentration device.
  • the organic amine effective components volatilized in the decarbonized gas can be recovered and reused, and the carbon dioxide in the steam enters the next condensation section for storage as the temperature of the desorption tower rises.
  • the heat of the recovered desorbed steam can be used to heat the desorption tower and reduce the energy consumption of the reboiler.
  • the reflux water and steam can realize the water replenishment function of the recovery system to maintain the high capture efficiency of the carbon capture solution.
  • an embodiment of the present disclosure further provides a method for recovering decarbonized gas after capture, which method can optionally be applied to the above-mentioned recovery system.
  • FIG3 is a flow chart of the method for recovering the captured decarbonized gas. As shown in FIG3 , the method includes:
  • Step 301 providing at least two chambers, each chamber containing activated carbon, wherein each chamber is connected to a carbon capture and absorption tower, and each chamber controls the flow direction of decarbonized gas output from the carbon capture and absorption tower via its own air inlet valve;
  • Step 302 in response to the decarbonized gas entering the chamber, determining the adsorption efficiency of the activated carbon in the chamber;
  • Step 303 When the adsorption efficiency of the activated carbon in the compartment is lower than a predetermined value, the air intake valve of the compartment is controlled to close and the air intake valve of another compartment is opened, so that the activated carbon in the other compartment can adsorb the decarbonized gas.
  • each compartment inputs high-temperature steam into the reboiler through its own steam input valve; after the air inlet valve of the compartment is closed, the steam input valve of the compartment is controlled to open so that the high-temperature steam from the reboiler enters the compartment to desorb the gas adsorbed by the activated carbon in the compartment.
  • the adsorption and desorption treatment of the decarbonized gas can be achieved, and the decarbonized gas can be recycled and reused, reducing resource waste and lowering the probability of pollution.
  • the method further comprises: returning the desorbed gas to the desorption tower in the form of steam.
  • the heat of the desorbed steam recovered through the desorption tower can be used to heat it, which can reduce the energy consumption of the reboiler.
  • the method further includes pre-installing an air supply blower, a three-way ventilation valve, and a burner; and after the cabin's air inlet valve is closed, transferring residual gas from the cabin after activated carbon adsorption to the burner via the air supply blower and the three-way ventilation valve.
  • the residual gas is clean air and can be transferred to the burner for further use, further improving resource utilization.
  • the high-temperature flue gas is discharged from the burner and pre-treated for desulfurization, denitrification and dust removal before entering the carbon dioxide absorption tower and being reversely contacted with the carbon capture solvent containing organic amines to be captured. Due to incomplete pretreatment and decarbonization reaction, the decarbonized gas will contain a large amount of gas components such as VOCs, organic amines volatilized from the absorbent, a small amount of uncaptured CO2 gas and moisture, etc., which causes waste of resources and also causes secondary pollution to the air.
  • gas components such as VOCs, organic amines volatilized from the absorbent, a small amount of uncaptured CO2 gas and moisture, etc.
  • the embodiment of the present disclosure uses activated carbon adsorption and concentration to replace the traditional water washing process for the decarbonized gas discharged from the absorption tower, thereby overcoming the problems of water resource consumption and power consumption in the water washing process.
  • the disclosed embodiments utilize the residual steam heat from the desorption tower reboiler to alternately desorb and regenerate the activated carbon in the multi-compartment activated carbon adsorption and concentration device.
  • the desorbed hot steam and condensed solution containing carbon and organic amines are then returned to the desorption tower, recovering and reusing the gas components in the decarbonized gas.
  • the heat from the desorption steam is recovered to heat the desorption tower, reducing reboiler energy consumption.
  • the reflux water and steam replenish the entire recovery system, maintaining the high capture efficiency of the carbon capture solution.
  • This embodiment further provides an electronic device, comprising a memory, a processor, and a computer program stored in the memory and executable on the processor.
  • the electronic device may be a desktop computer, a tablet computer, a mobile terminal, etc., but this embodiment is not limited thereto.
  • the electronic device may be implemented with reference to the above-described method embodiments and the above-described device/system embodiments, the contents of which are incorporated herein, and any repetitions are omitted.
  • the embodiment of the present disclosure further provides a computer-readable storage medium having a computer program stored thereon, which is used to implement the steps of the above-mentioned recycling method when executed by a processor.
  • the disclosed embodiment proposes a scheme for concentrating and recovering decarbonized gas after capture and reusing the residual steam in the reboiler.
  • the scheme uses the residual steam in the reboiler as a desorption heat source to efficiently recover the unabsorbed carbon dioxide, escaped organic amine absorbent and water in the decarbonized gas, thereby reducing the waste of effective resources, overcoming the problems of water resource consumption and power consumption in the water washing process in related technologies, and reducing the secondary pollution problem after the decarbonized gas is directly discharged.
  • the desorption liquid of the adsorption concentration device is refluxed.
  • the organic amines and other effective components volatilized in the decarbonized gas are recovered and reused, and the carbon dioxide in the steam enters the next condensation section for storage as the temperature of the desorption tower rises.
  • the heat of the desorption steam is recovered for heating the desorption tower, which can reduce the energy consumption of the reboiler.
  • the reflux water and steam can realize the water replenishment function for the entire system to maintain the high capture efficiency of the carbon capture solution.

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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)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

本公开公开了一种捕集后脱碳气体的回收方法、系统及活性炭浓缩装置，其中，所述装置对碳捕集吸收塔输出的脱碳气体进行回收处理，所述装置包括：至少两个舱室，各舱室中含有活性炭，所述各舱室通过各自的进气阀门控制所述脱碳气体的流向；活性炭吸附效率确定单元，用于确定各舱室中活性炭的吸附效率；进气阀门控制器，用于在舱室中活性炭的吸附效率低于预定值时，控制该舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。通过本公开，可以减少资源浪费，降低污染概率。

Description

捕集后脱碳气体的回收方法、系统及活性炭浓缩装置
相关申请的交叉引用
本公开基于申请号为202410121981.9、申请日为2024年01月29日的中国专利申请提出，并要求该中国专利申请的优先权，该中国专利申请的全部内容在此引入本申请作为参考。
技术领域
本公开涉及温室气体减排及资源化利用技术领域，具体涉及一种捕集后脱碳气体的回收方法、系统及活性炭浓缩装置。
背景技术
目前，能源部门排放的温室气体所占比重占68％，在其排放的温室气体中90％都是二氧化碳(CO2)，在众多CO2排放源中，煤和石油燃烧排放的CO2是全球CO2的主要来源。随着非工业国家的逐渐崛起，燃煤导致的CO2排放比重已增加至各排放源的第一位，其中电力行业二氧化碳排放量巨大，已占全国总二氧化碳排放量的45％。针对日益升高的温室气体排放量，我国发展了多项碳减排政策和针对性技术措施，如燃烧前捕集技术、富氧燃烧技术和燃烧后捕集技术等。其中燃烧后捕集技术是目前最为成熟的技术之一，已经在全球数百个地区建立示范工程，并且在逐步完善优化工艺的进程之中。
常用的捕集工艺采用对二氧化碳具有高度选择性的有机胺溶液进行吸收后升温再生，之后生成高纯度的二氧化碳储存起来。在该工艺中，经过有机溶剂吸收后的烟气经吸收塔顶排出。排出的残余量气体组分主要包括：VOCs(Volatile Organic Compounds，挥发性有机化合物)、吸收剂中挥发出的有机胺、少量未被捕获的CO2气体及水分等。
这些排出的残余量气体中不仅含有有害物质，还有可再利用的有机胺、CO2气体及水分等。直接将残余量气体排至大气中，不仅会造成资源的浪费，还会对空气造成二次污染。
发明内容
本公开提供一种捕集后脱碳气体的回收方法、系统及活性炭浓缩装置，以解决上述提及的至少一个问题。
根据本公开的第一方面，提供一种捕集后脱碳气体的活性炭浓缩装置，所述装置对碳捕集吸收塔输出的脱碳气体进行回收处理，所述装置包括：至少两个舱室，各舱室中含有活性炭，所述各舱室通过各自的进气阀门控制所述脱碳气体的流向；活性炭吸附效率确定单元，用于确定各舱室中活性炭的吸附效率；进气阀门控制器，用于在舱室中活性炭的吸附效率低于预定值时，控制该舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
进一步地，各舱室通过各自的蒸汽输入阀门输入再沸器的高温蒸汽，所述装置还包括：蒸汽输入阀门控制器，用于在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
进一步地，所述装置还包括：回流管道，用于将脱附处理后的气体以蒸汽方式回流至解吸塔。
可选地，所述装置还包括：送气风机、三通风阀和燃烧器，其中：在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。
根据本公开的第二方面，提供一种捕集后脱碳气体的回收系统，所述系统包括：上述的捕集后脱碳气体的活性炭浓缩装置、碳捕集吸收塔、再沸器以及解吸塔，其中，通过所述再沸器的加热处理，所述解吸塔将从所述碳捕集吸收塔进入的二氧化碳进行脱附处理。
可选地，所述解吸塔对从所述活性炭浓缩装置输出的以蒸汽方式回流的脱附处理后的气体进行回收处理，并基于蒸汽热量进行升温操作。
根据本公开的第三方面，提供一种捕集后脱碳气体的回收方法，所述方法包括：设置至少两个舱室，各舱室中含有活性炭，其中，所述各舱室与碳捕集吸收塔相连，所述各舱室通过各自的进气阀门控制从所述碳捕集吸收塔输出的脱碳气体的流向；响应于所述脱碳气体进入舱室，确定该舱室中活性炭的吸附效率；在所述舱室中活性炭的吸附效率低于预定值时，控制所述舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
进一步地，所述方法还包括：各舱室通过各自的蒸汽输入阀门输入再沸器的高温蒸汽；在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
可选地，所述方法还包括：将脱附处理后的气体以蒸汽方式回流至解吸塔。
可选地，所述方法还包括：预先设置送气风机、三通风阀和燃烧器；在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。
同时，本公开还提供一种计算机设备，包括存储器、处理器及存储在存储器上并可在处理器上运行的计算机程序，处理器执行计算机程序时实现上述方法。
同时，本公开还提供一种计算机可读存储介质，计算机可读存储介质存储有执行上述方法的计算机程序。
由上述技术方案可知，本技术方案通过设置含有活性炭的舱室，可以实现对脱碳气体的吸附处理和脱附处理，从而实现对脱碳气体的回收利用，从而可以减少资源浪费，降低污染概率。
为让本公开的上述和其他目的、特征和优点能更明显易懂，下文特举实施例，并配合所附图式，作详细说明如下。
附图说明
图1是本公开实施例的捕集后脱碳气体的回收系统的示意图。
图2是本公开实施例的捕集后脱碳气体的活性炭浓缩装置的结构框图。
图3是本公开实施例的捕集后脱碳气体的回收方法的流程图。
附图标记：
碳捕集吸收塔1、富液泵2、贫富液换热器3、贫液泵4、解吸塔5、再沸器6、舱室7、进气控制阀8、蒸汽脱附控制阀9、送气风机10、三通风阀11、燃烧器12、燃烧后捕集装置13、活性炭浓缩装置14、活性炭吸附效率确定单元142、进气阀门控制器143。
具体实施方式
下面将结合本公开实施例中的附图，对本公开实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本公开一部分实施例，而不是全部的实施例。基于本公开中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本公开保护的范围。
在相关技术中，从吸收塔排出的残余量气体(也可以称为脱碳气体)中不仅含有有害物质，还有可再利用的有机胺、CO2气体及水分。如果直接将残余量气体排出至大气中，不仅会造成资源的浪费，还会对空气造成二次污染。
基于此，本公开实施例提供一种捕集后脱碳气体的回收方案，该方案一方面可以对脱碳气体中的气体组分进行回收再利用，减少资源浪费，降低污染概率；另一方面回收脱附蒸汽的热量可用于解吸塔升温，可以降低再沸器的能耗。
以下结合附图对本公开实施例进行详细的描述。
图1是根据本公开实施例的捕集后脱碳气体回收系统的示意图，如图1所示，该系统包括：燃烧后捕集装置13和捕集后脱碳气体的活性炭浓缩装置14。其中，活性炭浓缩装置14对燃烧后捕集装置13捕集后的脱碳气体进行回收处理。
图2是该活性炭浓缩装置14的结构框图，如图2所示，该活性炭浓缩装置14包括：至少两个舱室7、活性炭吸附效率确定单元142和进气阀门控制器143，其中：
各舱室中含有活性炭，活性炭可以吸附脱碳气体。所述各舱室通过各自的进气阀门控制所述脱碳气体的流向。
活性炭吸附效率确定单元142，用于确定各舱室中活性炭的吸附效率。
在实际操作中，活性炭吸附效率确定单元142可以是设置在舱室进出口的两个气体分析仪，用于测量气体(例如，CO及CO2)浓度，并根据进出口气体的浓度差确定舱室中活性炭的吸附效率。
进气阀门控制器143，用于在舱室中活性炭的吸附效率低于预定值(预定值可以依据实际情况而定，本公开对此不作限制)时，控制该舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
进一步地，各舱室还可以通过各自的蒸汽输入阀门输入再沸器的高温蒸汽。相应地，活性炭浓缩装置14还包括：蒸汽输入阀门控制器，用于在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
在实际操作中，活性炭浓缩装置14还包括：回流管道，用于将脱附处理后的气体以蒸汽方式回流至解吸塔。脱附处理后的气体主要包括：可再利用的有机胺、CO2气体等。之后，解吸塔可以对这些气体进行回收处理。
在一个实施例中，活性炭浓缩装置14还包括：送气风机、三通风阀和燃烧器，其中：在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。这些剩余气体为洁净空气，可以输入至燃烧器继续利用。
为了更好地理解本公开，以下结合图1来详细描述回收系统的工作原理。
继续参考图1，燃烧后捕集装置13包括：碳捕集吸收塔1、富液泵2、贫富液换热器3、贫液泵4、解吸塔5以及再沸器6；活性炭浓缩装置14包括：舱室7、进气控制阀8、蒸汽脱附控制阀9、送气风机10、三通风阀11以及燃烧器12。
在回收系统工作时，通过再沸器6的加热处理，解吸塔5将对碳捕集吸收塔1进入的二氧化碳进行脱附处理。碳捕集吸收塔1中的脱碳气体进入活性炭浓缩装置14进行脱碳气体的吸附和脱附处理，随后，解吸塔5对从活性炭浓缩装置14的舱室7输出的以蒸汽方式回流的脱附处理后的气体进行回收处理，并基于蒸汽热量进行升温操作。
通过对活性炭浓缩装置14对脱碳气体的吸附和脱附处理，解吸塔5对脱附处理后的气体进行回收处理，可以对脱碳气体中的气体组分进行回收再利用，减少资源浪费，降低污染概率。同时，解吸塔5基于蒸汽热量进行升温操作，可以降低再沸器的能耗。
在实际操作中，电厂烟气自燃烧炉排出后经过脱硫脱硝除尘预处理后进入碳捕集吸收塔1中，自下而上与碳捕集溶剂贫液进行充分接触，烟气中的二氧化碳被贫液(贫液由贫液泵4产生)吸收后在重力作用下落至塔底，在富液泵2的动力下进入贫富液换热器3中与热贫液进行充分换热预升温后，溶液进入二氧化碳解吸塔5中，在再沸器6的作用下进行升温加热，二氧化碳及部分水蒸气被脱附，自解吸塔5塔顶排出进入冷凝器进行后续处理系统。吸收塔1中产生的脱碳气体自吸收塔1塔顶通过进气控制阀8(具有上述进气阀门控制器的功能)进入活性炭浓缩装置的舱室7，利用舱室中活性炭多孔结构和良好的吸附性能吸收未完全吸收的二氧化碳气体、一氧化碳气体及脱碳气体中的其他成分。之后，吸附后的洁净空气通过送气风机10和三通风阀11控制，一部分补入锅炉燃烧器12，一部分正常排空。
上述舱室7为二室或者多室结构，当一室进气阀开启时，该舱室进行烟气吸附工作。之后，根据舱室进出口气体分析数据，测试一氧化碳(CO)和二氧化碳浓度(CO2)，以此判断活性炭吸附效率。具体而言，可以在舱室7的进出口设置两个气体分析仪，用于测量CO及CO2浓度，根据进出口的气体浓度差确定舱室内活性炭的吸附效率。
在吸附一段时间待吸附效率降低至50％～60％时，该舱室的进气阀门关闭，同时另一舱室的进气阀门开启，继续进行气体吸附工作。同时，再沸器6的剩余蒸汽通过保温管路经由蒸汽脱附控制阀9引入该舱室内，用高温蒸汽对活性炭孔道中的气体组分进行脱附再生，吹脱后的携带二氧化碳的蒸汽以及回落至舱底的水液通过管路(即，上述的回流管道)进入解吸塔5中。待舱室中的活性炭脱附结束，另一舱室活性炭吸附效率趋近50％～60％时，另一舱室的进气阀门关闭，该舱室的进气阀门开启，循环往复，保持多舱室同步吸附脱附工作。如此，可以提高脱碳气体回收处理的效率。
在实际操作中，进气阀门和蒸汽脱附控制阀门可以是电动的，阀门的开关可以是电动阀PLC(Programmable Logic Controller，可编程序控制器)手动控制。
在实际操作中，活性炭浓缩装置14可以依实际场景设置2～N个舱室，多舱室之间通过阀门控制气体流向，采用分区吸附分区脱附的方式进行多舱室同步工作，无暂停设备运行进行脱附的风险，这样可以保证工作效率。
本公开实施例采用活性炭吸附浓缩的方式取代传统水洗塔对脱碳尾气(即，脱碳气体)的处理工艺，高效回收并分离脱碳尾气中未吸收完全的二氧化碳、逸散的有机胺吸收剂及水份等，降低了有效资源的浪费以及水洗工艺中水资源的消耗和电耗。同时，通过利用活性炭对有机物高效的捕获性能，吸收尾气中的其他气体成分，可以防止直排后对空气造成的二次污染。
另外，本公开实施例充分利用二氧化碳捕集后蒸汽再生的剩余蒸汽热量，对活性炭孔洞中吸附的气体分子进行加热蒸汽脱附再生，恢复活性炭吸附性能，同时用高温蒸汽将孔洞内吸附的CO2、有机胺等成分以蒸汽的形式回收，并回流至解吸塔内，这样不会产生多余废液，减少了废水废物二次处理的成本。
也就是说，本公开实施例将活性炭浓缩装置脱附液体进行回流，一方面可以对脱碳气体中挥发出的有机胺有效成分进行回收再利用，蒸汽中的二氧化碳随解吸塔的升温进入下一冷凝工段进行储存，另一方面回收脱附蒸汽的热量可以用于解吸塔升温，降低再沸器能耗，与此同时回流水和蒸汽可以对回收系统实现补水功能，用以保持碳捕集溶液的高效捕集效率。
基于相似的构思，本公开实施例还提供一种捕集后脱碳气体的回收方法，该方法可选地可应用于上述的回收系统。
图3是该捕集后脱碳气体回收方法的流程图，如图3所示，该方法包括：
步骤301，设置至少两个舱室，各舱室中含有活性炭，其中，各舱室与碳捕集吸收塔相连，所述各舱室通过各自的进气阀门控制从所述碳捕集吸收塔输出的脱碳气体的流向；
步骤302，响应于所述脱碳气体进入舱室，确定该舱室中活性炭的吸附效率；
步骤303，在所述舱室中活性炭的吸附效率低于预定值时，控制所述舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
进一步地，上述方法还包括：各舱室通过各自的蒸汽输入阀门输入再沸器的高温蒸汽；在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
通过设置含有活性炭的舱室，可以实现对脱碳气体的吸附处理和脱附处理，可以实现对脱碳气体的回收再利用，减少资源浪费，降低污染概率。
在一个实施例中，上述方法还包括：将脱附处理后的气体以蒸汽方式回流至解吸塔。
通过解吸塔回收脱附蒸汽的热量可用于其升温，可以降低再沸器的能耗。
在一个实施例中，上述方法还包括：预先设置送气风机、三通风阀和燃烧器；在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。这里的剩余气体为洁净空气，可以输入至燃烧器继续利用，进一步提高了资源利用率。
上述各步骤的具体执行过程，可以参见上述系统实施例中的描述，此处不再赘述。
在实施本公开实施例之前，高温烟气自燃烧器排出后经过脱硫脱硝除尘预处理后，进入二氧化碳吸收塔与含有机胺的碳捕集溶剂逆向接触从而被捕获，脱碳气体由于预处理及脱碳反应不完全，会含大量气体组分如VOCs、吸收剂中挥发出的有机胺、少量未被捕获的CO2气体及水分等，这造成了资源的浪费，同时还会对空气造成二次污染。为减少吸收塔的资源浪费，降低污染概率，以及充分考虑后续工艺中的资源再利用问题，本公开实施例将吸收塔排出的脱碳气体采用活性炭吸附浓缩的方式，取代传统水洗工艺，克服了水洗工艺中水资源消耗和电耗的问题。同时，本公开实施例利用解吸塔再沸器的剩余蒸汽热量，交替对多舱室活性炭吸附浓缩装置中的活性炭进行蒸汽脱附再生，脱附下来的含碳、有机胺的含热蒸汽及冷凝溶液回流至解吸塔内，一方面对脱碳气体中的气体组分进行回收再利用，另一方面回收脱附蒸汽的热量用于解吸塔升温，降低了再沸器能耗。与此同时，回流水和蒸汽可以对整个回收系统实现补水功能，可以保持碳捕集溶液的高效捕集效率。
本实施例还提供一种电子设备，该电子设备包括存储器、处理器及存储在存储器上并可在处理器上运行的计算机程序。该电子设备可以是台式计算机、平板电脑及移动终端等，本实施例不限于此。在本实施例中，该电子设备可以参照上述方法实施例进行实施及上述装置/系统的实施例进行实施，其内容被合并于此，重复之处不再赘述。
本公开实施例还提供一种计算机可读存储介质，其上存储有计算机程序，该计算机程序被处理器执行时以实现上述回收方法的步骤。
综上所述，本公开实施例提出了一种捕集后脱碳气体浓缩回收及再沸器剩余蒸汽再利用的方案，该方案利用再沸器剩余蒸汽作为脱附热源，高效回收脱碳气体中未吸收完全的二氧化碳、逸散的有机胺吸收剂及水份等，降低了有效资源的浪费，克服了相关技术中水洗工艺中水资源的消耗和电耗的问题，也减少了脱碳气体直排后的二次污染问题。同时，将吸附浓缩装置脱附液体进行回流，一方面对脱碳气体中挥发出的有机胺等有效成分进行回收再利用，蒸汽中的二氧化碳随解吸塔的升温进入下一冷凝工段进行储存，另一方面回收脱附蒸汽的热量用于解吸塔升温，可以降低再沸器能耗，与此同时回流水和蒸汽可以对整个系统实现补水功能，用以保持碳捕集溶液的高效捕集效率。
本公开中应用了具体实施例对本公开的原理及实施方式进行了阐述，以上实施例的说明只是用于帮助理解本公开的方法及其核心思想；同时，对于本领域的一般技术人员，依据本公开的思想，在具体实施方式及应用范围上均会有改变之处，综上所述，本说明书内容不应理解为对本公开的限制。

Claims (10)

  1. 一种捕集后脱碳气体的活性炭浓缩装置，所述装置对碳捕集吸收塔输出的脱碳气体进行回收处理，所述装置包括：
    至少两个舱室，各舱室中含有活性炭，所述各舱室通过各自的进气阀门控制所述脱碳气体的流向；
    活性炭吸附效率确定单元，用于确定各舱室中活性炭的吸附效率；
    进气阀门控制器，用于在舱室中活性炭的吸附效率低于预定值时，控制该舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
  2. 根据权利要求1所述的捕集后脱碳气体的活性炭浓缩装置，其中各舱室通过各自的蒸汽输入阀门输入再沸器的高温蒸汽，所述装置还包括：
    蒸汽输入阀门控制器，用于在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
  3. 根据权利要求2所述的捕集后脱碳气体的活性炭浓缩装置，还包括回流管道，所述回流管道用于将脱附处理后的气体以蒸汽方式回流至解吸塔。
  4. 根据权利要求1-3中任一项所述的捕集后脱碳气体的活性炭浓缩装置，还包括送气风机、三通风阀和燃烧器，其中：
    在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。
  5. 一种捕集后脱碳气体的回收系统，包括：如权利要求1至4中任一项所述的捕集后脱碳气体的活性炭浓缩装置、碳捕集吸收塔、再沸器以及解吸塔，其中，通过所述再沸器的加热处理，所述解吸塔将从所述碳捕集吸收塔进入的二氧化碳进行脱附处理。
  6. 根据权利要求5所述的捕集后脱碳气体的回收系统，其中所述解吸塔对从所述活性炭浓缩装置输出的以蒸汽方式回流的脱附处理后的气体进行回收处理，并基于蒸汽热量进行升温操作。
  7. 一种捕集后脱碳气体的回收方法，包括：
    设置至少两个舱室，各舱室中含有活性炭，其中，所述各舱室与碳捕集吸收塔相连，所述各舱室通过各自的进气阀门控制从所述碳捕集吸收塔输出的脱碳气体的流向；
    响应于所述脱碳气体进入舱室，确定该舱室中活性炭的吸附效率；
    在所述舱室中活性炭的吸附效率低于预定值时，控制所述舱室的进气阀门关闭并打开另一舱室的进气阀门，以便于所述另一舱室中的活性炭对所述脱碳气体进行吸附处理。
  8. 根据权利要求7所述的捕集后脱碳气体的回收方法，还包括：
    各舱室通过各自的蒸汽输入阀门输入再沸器的高温蒸汽；
    在舱室的进气阀门关闭后，控制该舱室的蒸汽输入阀门打开，以便于所述再沸器的高温蒸汽进入该舱室，对该舱室中活性炭吸附到的气体进行脱附处理。
  9. 根据权利要求8所述的捕集后脱碳气体的回收方法，还包括：
    将脱附处理后的气体以蒸汽方式回流至解吸塔。
  10. 根据权利要求7-9中任一项所述的捕集后脱碳气体的回收方法，还包括：
    预先设置送气风机、三通风阀和燃烧器；
    在舱室的进气阀门关闭后，将该舱室经过活性炭吸附后的剩余气体通过所述送气风机和三通风阀输入至所述燃烧器。
PCT/CN2025/074093 2024-01-29 2025-01-22 捕集后脱碳气体的回收方法、系统及活性炭浓缩装置 Pending WO2025162151A1 (zh)

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CN203899399U (zh) * 2014-03-27 2014-10-29 北京日新达能技术有限公司 新型有机气体活性炭纤维多级吸附净化回收装置
JP2019069417A (ja) * 2017-10-10 2019-05-09 株式会社日立製作所 排ガスからの二酸化炭素回収方法及び設備
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CN117959888A (zh) * 2024-01-29 2024-05-03 中国华能集团清洁能源技术研究院有限公司 捕集后脱碳气体的回收方法、系统及活性炭浓缩装置

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CN117959888A (zh) * 2024-01-29 2024-05-03 中国华能集团清洁能源技术研究院有限公司 捕集后脱碳气体的回收方法、系统及活性炭浓缩装置

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