WO2026001067A1 - 二氧化碳捕集装置 - Google Patents

二氧化碳捕集装置

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Publication number
WO2026001067A1
WO2026001067A1 PCT/CN2025/080764 CN2025080764W WO2026001067A1 WO 2026001067 A1 WO2026001067 A1 WO 2026001067A1 CN 2025080764 W CN2025080764 W CN 2025080764W WO 2026001067 A1 WO2026001067 A1 WO 2026001067A1
Authority
WO
WIPO (PCT)
Prior art keywords
inlet
outlet
dehydration
carbon dioxide
regeneration
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/CN2025/080764
Other languages
English (en)
French (fr)
Inventor
刘牛
曹枝阳
徐向和
席喜勤
马骏骁
王焕君
范紫桉
鄞铃
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.)
Huaneng Clean Energy Research Institute
Huaneng Group Technology Innovation Center Co Ltd
Zhengning Power Plant of Huaneng Longdong Energy Co Ltd
Original Assignee
Huaneng Clean Energy Research Institute
Huaneng Group Technology Innovation Center Co Ltd
Zhengning Power Plant of Huaneng Longdong Energy Co Ltd
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Filing date
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Application filed by Huaneng Clean Energy Research Institute, Huaneng Group Technology Innovation Center Co Ltd, Zhengning Power Plant of Huaneng Longdong Energy Co Ltd filed Critical Huaneng Clean Energy Research Institute
Publication of WO2026001067A1 publication Critical patent/WO2026001067A1/zh
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—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

Definitions

  • This disclosure relates to the field of carbon dioxide absorption technology, and more specifically, to a carbon dioxide capture device.
  • phase change chemical absorption is a major method for CO2 recovery.
  • the carbon capture system includes an absorption module and a regeneration tower. Flue gas is introduced into the absorption module, where an absorbent absorbs the CO2 . In the regeneration tower, the CO2 -absorbed solution is desorbed, and the CO2 product is obtained in subsequent processes.
  • This disclosure provides a carbon dioxide capture device to solve the problem in related technologies that the rich liquid does not undergo phase separation after absorbing carbon dioxide.
  • a carbon dioxide capture device comprising: a dehydration tower containing a desiccant for drying flue gas, the dehydration tower having a dehydration inlet and a dehydration outlet connected to each other, the dehydration inlet being connected to a gas source; an absorption assembly having an air inlet and an air outlet connected to each other, as well as an absorbent inlet and an absorbent outlet connected to each other, the air inlet being connected to the dehydration outlet and the air outlet being connected to the outside; a regeneration tower having an exhaust outlet and a regeneration inlet and a regeneration outlet connected to each other, the regeneration inlet being connected to the absorbent outlet and the regeneration outlet being connected to the absorbent inlet; and a heater having a heating inlet and a heating outlet, the heating inlet being connected to the gas source and the heating outlet being connected to the dehydration outlet.
  • the carbon dioxide capture device further includes a cooler and a separator, the cooler having a cooling inlet and a cooling outlet connected in communication, and the separator having a separation inlet, the cooling inlet being connected to a dehydration inlet, and the cooling outlet being connected to a separation inlet.
  • the cooler further includes a heat exchange inlet and a heat exchange outlet connected together, the heat exchange inlet being connected to the absorbent outlet and the heat exchange outlet being connected to the regeneration inlet.
  • the carbon dioxide capture device further includes a pre-wash tower having a pre-wash condensation inlet and a flue gas inlet and a flue gas outlet connected thereto.
  • the flue gas inlet is connected to a gas source, and the dehydration inlet is connected to the flue gas outlet.
  • the separator also has a separation outlet and a reflux pipe connected to the separation outlet, and the outlet of the reflux pipe is connected to the pre-wash condensation inlet.
  • the carbon dioxide capture device further includes a water washing tower, which has a water washing condensation inlet and a decarbonized gas inlet and a decarbonized gas outlet connected thereto.
  • the decarbonized gas inlet is connected to the gas outlet, and the decarbonized gas outlet is connected to the outside.
  • the separator also has a separation outlet and a reflux pipe connected to the separation outlet. The outlet of the reflux pipe is connected to the water washing condensation inlet.
  • the carbon dioxide capture device further includes a water storage tank disposed on the return pipe.
  • each dehydration tower there are three dehydration towers.
  • the dehydration outlet of each dehydration tower is connected to the heating outlet and the air inlet, respectively.
  • the dehydration inlet of each dehydration tower is connected to the air source and the cooling inlet, respectively.
  • a shut-off valve is provided on the connecting pipes between the dehydration outlet and the heating outlet, the connecting pipe between the dehydration outlet and the air inlet, the connecting pipe between the dehydration inlet and the air source, and the connecting pipe between the dehydration inlet and the cooling inlet.
  • the absorption assembly includes an absorption tower and a phase separator connected in series, with an air inlet, an air outlet, and an absorbent inlet located in the absorption tower, and an absorbent outlet located in the phase separator.
  • the carbon dioxide capture device further includes a rich-lean liquid heat exchanger having a rich liquid inlet and a rich liquid outlet connected together, and a lean liquid inlet and a lean liquid outlet connected together.
  • the rich liquid inlet is connected to the absorbent outlet
  • the rich liquid outlet is connected to the regeneration inlet
  • the lean liquid inlet is connected to the regeneration outlet
  • the lean liquid outlet is connected to the absorbent inlet.
  • the carbon dioxide capture device further includes a reboiler having a reboiler inlet and a reboiler outlet connected together, and a heating inlet and a heating outlet connected together.
  • the reboiler outlet is connected to the regeneration inlet
  • the regeneration outlet is connected to the reboiler inlet
  • the heating inlet is connected to a heat source.
  • the carbon dioxide capture device includes a dehydration tower, an absorption assembly, a regeneration tower, and a heater. Flue gas is conveyed into the dehydration tower through its dehydration inlet, where a desiccant dries the flue gas. The dried flue gas then enters the absorption assembly through its dehydration outlet and inlet. The absorbent in the absorption assembly absorbs the carbon dioxide in the flue gas, forming a rich liquid. The flue gas, after carbon dioxide removal, is discharged through its outlet. The rich liquid undergoes phase separation and enters the regeneration tower through its absorbent outlet and regeneration inlet. In the regeneration tower, the rich liquid is heated and desorbed, and the desorbed carbon dioxide is discharged through its exhaust outlet.
  • the rich liquid is then converted into a lean liquid containing absorbent, which is returned to the absorption assembly through its regeneration outlet and absorbent inlet.
  • the heater can heat the flue gas, allowing it to enter the dehydration tower through its dehydration outlet to dry the moisture-absorbing desiccant, enabling the desiccant to be recycled. Because the moisture in the flue gas is dried using a desiccant in the dehydration tower, the moisture content in the flue gas is reduced. This ensures that the flue gas does not affect the water balance of the system after entering the absorption module, and allows for smooth phase separation.
  • Figure 1 shows a schematic diagram of the structure of a carbon dioxide capture device provided according to an embodiment of the present disclosure.
  • the above figures include the following reference numerals: 10. Dehydration tower; 11. Shut-off valve; 20. Absorption assembly; 21. Absorption tower; 22. Phase separator; 30. Regeneration tower; 40. Heater; 50, Cooler; 60, Separator; 70, Pre-washing tower; 80, Water washing tower; 90, Water storage tank; 100, Lean/rich liquid heat exchanger; 110, Reboiler.
  • this embodiment of the present disclosure provides a carbon dioxide capture device, which includes a dehydration tower 10, an absorption assembly 20, a regeneration tower 30, and a heater 40.
  • the dehydration tower 10 is provided with a desiccant for drying flue gas and has a dehydration inlet and a dehydration outlet connected to each other, with the dehydration inlet connected to a gas source.
  • the absorption assembly 20 has an air inlet and an air outlet connected to each other, as well as an absorbent inlet and an absorbent outlet connected to each other, with the air inlet connected to the dehydration outlet and the air outlet connected to the outside.
  • the regeneration tower 30 has an exhaust port and a regeneration inlet and a regeneration outlet connected to each other, with the regeneration inlet connected to the absorbent outlet and the regeneration outlet connected to the absorbent inlet.
  • the heater 40 has a heating inlet and a heating outlet, with the heating inlet connected to the gas source and the heating outlet connected to the dehydration outlet.
  • the carbon dioxide capture device includes a dehydration tower 10, an absorption assembly 20, a regeneration tower 30, and a heater 40.
  • Flue gas is conveyed into the dehydration tower 10 through its dehydration inlet, where a desiccant dries the flue gas.
  • the dried flue gas then enters the absorption assembly 20 through its dehydration outlet and inlet.
  • the absorbent in the absorption assembly 20 absorbs the carbon dioxide in the flue gas, forming a rich liquid.
  • the flue gas after carbon dioxide removal, is discharged through its outlet.
  • the rich liquid undergoes phase separation and enters the regeneration tower 30 through its absorbent outlet and regeneration inlet.
  • the rich liquid is heated and desorbed within the regeneration tower 30, and the desorbed carbon dioxide is discharged through its exhaust outlet.
  • the rich liquid is transformed into a lean liquid containing absorbent, which is returned to the absorption assembly 20 through its regeneration outlet and absorbent inlet.
  • the heater 40 heats the flue gas, allowing it to enter the dehydration tower 10 through its dehydration outlet to dry the moisture-absorbing desiccant, enabling the desiccant to be recycled. Since the moisture in the flue gas is dried by the desiccant in the dehydration tower 10, the moisture content in the flue gas is reduced, so that the water balance of the system will not be affected after the flue gas enters the absorption component 20, and phase separation can occur smoothly.
  • the carbon dioxide capture device also includes a cooler 50 and a separator 60.
  • the cooler 50 has a cooling inlet and a cooling outlet connected together, and the separator 60 has a separation inlet.
  • the cooling inlet is connected to the dehydration inlet, and the cooling outlet is connected to the separation inlet. After regeneration and hot blowing, the flue gas enters the cooler 50 through the dehydration inlet.
  • the cooler 50 can cool the high-temperature flue gas so that gas and water can be separated in the separator 60.
  • the cooler 50 also includes a heat exchange inlet and a heat exchange outlet connected together.
  • the heat exchange inlet is connected to the absorbent outlet, and the heat exchange outlet is connected to the regeneration inlet.
  • the regeneration hot-blown flue gas contains a large amount of moisture, which needs to be cooled to separate the moisture.
  • the regeneration hot-blown flue gas is sent into the cooler 50, where it is cooled by the low-temperature rich liquid (40°C to 50°C) from the absorbent outlet, thereby separating the moisture from the regeneration hot-blown flue gas.
  • the low-temperature rich liquid from the absorbent outlet also utilizes the heat from the regeneration hot-blown flue gas; the heated rich liquid is then sent to the regeneration tower for regeneration, reducing regeneration energy consumption.
  • the flue gas after regeneration and hot blowing, the flue gas enters the cooler 50 through the dehydration inlet and the cooling inlet, and the rich liquid enters the cooler 50 through the absorbent outlet and the heat exchange inlet.
  • the flue gas heats the rich liquid, and the heated rich liquid is then transported to the regeneration tower 30.
  • the carbon dioxide capture device also includes a pre-washing tower 70.
  • the pre-washing tower 70 has a pre-washing condensate inlet and connected flue gas inlet and outlet.
  • the flue gas inlet is connected to a gas source, and the dehydration inlet is connected to the flue gas outlet.
  • the separator 60 also has a separation outlet and a return pipe connected to the separation outlet. The outlet of the return pipe is connected to the pre-washing condensate inlet.
  • the pre-washing tower 70 can wash the flue gas containing carbon dioxide to purify it.
  • the condensate after separation in the separator 60 can enter the pre-washing tower 70 through the separation outlet, return pipe, and pre-washing condensate inlet, providing a water source for the pre-washing tower 70 and allowing the condensate to be recycled.
  • the carbon dioxide capture device also includes a water scrubbing tower 80.
  • the water scrubbing tower 80 has a water scrubbing condensate inlet and connected to a decarbonized gas inlet and outlet.
  • the decarbonized gas inlet is connected to the gas outlet, and the decarbonized gas outlet is connected to the outside.
  • the separator 60 also has a separation outlet and a return pipe connected to the separation outlet. The outlet of the return pipe is connected to the water scrubbing condensate inlet.
  • the water scrubbing tower 80 can wash the decarbonized flue gas to ensure it meets emission requirements.
  • the condensate after separation in the separator 60 can enter the water scrubbing tower 80 through the separation outlet, return pipe, and water scrubbing condensate inlet, providing a water source for the water scrubbing tower 80 and allowing the condensate to be recycled.
  • the carbon dioxide capture device also includes a water storage tank 90, which is installed on the return pipe.
  • the water storage tank 90 allows for the recovery and storage of condensate from the separator 60 for further use.
  • each dehydration tower 10 there are three dehydration towers 10.
  • the dehydration outlet of each dehydration tower 10 is connected to both the heating outlet and the air inlet
  • the dehydration inlet of each dehydration tower 10 is connected to both the air source and the cooling inlet.
  • Shut-off valves 11 are installed on the connecting pipes between the dehydration outlet and the heating outlet, the dehydration outlet and the air inlet, the dehydration inlet and the air source, and the dehydration inlet and the cooling inlet.
  • flue gas containing carbon dioxide enters the first dehydration tower 10 through the dehydration inlet.
  • the desiccant in the first dehydration tower 10 dries the flue gas.
  • the dried flue gas is then introduced into the absorption assembly 20 through the dehydration outlet and inlet for carbon dioxide adsorption.
  • the flue gas containing carbon dioxide is heated by the heater 40.
  • the heated flue gas then enters the second dehydration tower 10 through the dehydration outlet.
  • This high-temperature flue gas dries the moisture-absorbing desiccant.
  • the dried flue gas then enters the cooler 50 through the dehydration inlet and cooling inlet.
  • the rich liquid enters the cooler 50 through the absorbent outlet and heat exchange inlet, where the flue gas heats the rich liquid.
  • the flue gas containing carbon dioxide enters the third dehydration tower 10 through the dehydration inlet.
  • This flue gas cools the dried desiccant, allowing for its reuse.
  • the cooled flue gas is then introduced into the absorption assembly 20 through the dehydration outlet and inlet for carbon dioxide adsorption.
  • the absorption assembly 20 includes an absorption tower 21 and a phase separator 22 connected to each other.
  • the air inlet, air outlet, and absorbent inlet are located in the absorption tower 21, and the absorbent outlet is located in the phase separator 22.
  • the absorption tower 21 can absorb carbon dioxide in the flue gas, which then enters the phase separator 22 for phase separation and enters the regeneration tower 30 from the phase separator 22.
  • the absorbent is placed inside the absorption tower 21, and the rich liquid after absorbing carbon dioxide undergoes phase separation in the phase separator 22.
  • the carbon dioxide capture device also includes a lean-rich liquid heat exchanger 100.
  • the lean-rich liquid heat exchanger 100 has a rich liquid inlet and a rich liquid outlet connected together, as well as a lean liquid inlet and a lean liquid outlet connected together.
  • the rich liquid inlet is connected to the absorbent outlet
  • the rich liquid outlet is connected to the regeneration inlet
  • the lean liquid inlet is connected to the regeneration outlet
  • the lean liquid outlet is connected to the absorbent inlet.
  • the carbon dioxide capture device also includes a reboiler 110, which has a reboiler inlet and a reboiler outlet connected to each other, as well as a heating inlet and a heating outlet connected to each other.
  • the reboiler outlet is connected to the regeneration inlet
  • the regeneration outlet is connected to the reboiler inlet
  • the heating inlet is connected to a heat source.
  • the reboiler 110 can be used to reheat the rich liquid in the regeneration tower 30, so that carbon dioxide can be rapidly released from the rich liquid.
  • the flue gas comes into contact with and is adsorbed by the absorbent as it rises within the absorption tower 21, and its temperature gradually decreases.
  • the regeneration inlet is located at the upper part and the regeneration outlet at the bottom. The rich solution descends in the regeneration tower 30, releasing carbon dioxide, and its temperature gradually increases.
  • spatial relative terms such as “above,” “on top of,” “on the upper surface of,” “above,” etc., are used herein to describe the spatial positional relationship of a device or feature as shown in the figures to other devices or features. It should be understood that spatial relative terms are intended to encompass different orientations in use or operation beyond the orientation of the device as described in the figures. For example, if the device in the figures were inverted, a device described as “above” or “on top of” other devices or structures would subsequently be positioned as “below” or “under” other devices or structures. Thus, the exemplary term “above” can include both “above” and “below.” The device may also be positioned in other different ways (rotated 90 degrees or in other orientations), and the spatial relative descriptions used herein will be interpreted accordingly.

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  • Engineering & Computer Science (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

本公开提供了一种二氧化碳捕集装置，二氧化碳捕集装置包括：脱水塔，脱水塔内设置有干燥烟气的干燥剂，脱水塔具有相连通的脱水进口和脱水出口，脱水进口与气源连通；吸收组件，具有相连通的进气口和出气口以及相连通的吸收液进口和吸收液出口，进气口与脱水出口连通，出气口与外界连通；再生塔，具有排气口以及相连通的再生进口和再生出口，再生进口与吸收液出口连通，再生出口与吸收液进口连通；加热器，加热器具有加热进口和加热出口，加热进口与气源连通，加热出口与脱水出口连通。通过本公开提供的技术方案，能够解决相关技术中的吸收二氧化碳后的富液不发生分相的问题。

Description

二氧化碳捕集装置
相关申请的交叉引用
本公开基于申请号为202410839803.X、申请日为2024年06月26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公开作为参考。
技术领域
本公开涉及二氧化碳吸收技术领域，具体而言，涉及一种二氧化碳捕集装置。
背景技术
随着全球日益变暖，对人类的生产和生活造成了极大的困扰，尤其CO2是造成气温上升的主要罪魁祸首。因此，工业生产中，废气排放前CO2的处理至关重要。
在相关技术中，相变型化学吸收法回收CO2是一种主要的技术手段。碳捕集系统包括吸收组件和再生塔，通过将烟气导入至吸收组件，利用吸收剂对烟气中的CO2进行吸收，在再生塔中将吸收CO2后的溶液进行解吸，并在后续工序中得到CO2产品。
然而，由于烟气中的水分较高，随着运行时间的增加，烟气中水分进入吸收剂溶液中，相变体系中水分的逐渐增加会导致系统内水平衡被打破，从而不发生分相。
发明内容
本公开提供一种二氧化碳捕集装置，以解决相关技术中的吸收二氧化碳后的富液不发生分相的问题。
本公开提供了一种二氧化碳捕集装置，二氧化碳捕集装置包括：脱水塔，脱水塔内设置有干燥烟气的干燥剂，脱水塔具有相连通的脱水进口和脱水出口，脱水进口与气源连通；吸收组件，具有相连通的进气口和出气口以及相连通的吸收液进口和吸收液出口，进气口与脱水出口连通，出气口与外界连通；再生塔，具有排气口以及相连通的再生进口和再生出口，再生进口与吸收液出口连通，再生出口与吸收液进口连通；加热器，加热器具有加热进口和加热出口，加热进口与气源连通，加热出口与脱水出口连通。
在一些实施例中，二氧化碳捕集装置还包括冷却器和分离器，冷却器具有相连通的冷却进口和冷却出口，分离器具有分离进口，冷却进口与脱水进口连通，冷却出口与分离进口连通。
在一些实施例中，冷却器还包括相连通的换热进口和换热出口，换热进口与吸收液出口连通，换热出口与再生进口连通。
在一些实施例中，二氧化碳捕集装置还包括预洗塔，预洗塔具有预洗冷凝进口以及相连通的烟气进口和烟气出口，烟气进口与气源连通，脱水进口与烟气出口连通，分离器还具有分离出口以及与分离出口相连通的回流管，回流管的出口与预洗冷凝进口连通。
在一些实施例中，二氧化碳捕集装置还包括水洗塔，水洗塔具有水洗冷凝进口以及相连通的脱碳气进口、脱碳气出口，脱碳气进口与出气口连通，脱碳气出口与外界连通，分离器还具有分离出口以及与分离出口相连通的回流管，回流管的出口与水洗冷凝进口连通。
在一些实施例中，二氧化碳捕集装置还包括储水槽，储水槽设置在回流管上。
在一些实施例中，脱水塔为三个，每个脱水塔的脱水出口分别与加热出口以及进气口连通，每个脱水塔的脱水进口分别与气源以及冷却进口连通，脱水出口与加热出口的连通管路、脱水出口与进气口的连通管路、脱水进口与气源的连通管路、脱水进口与冷却进口的连通管路上均设置有关闭阀。
在一些实施例中，吸收组件包括相连通的吸收塔和分相器，进气口、出气口以及吸收液进口设置于吸收塔，吸收液出口设置于分相器。
在一些实施例中，二氧化碳捕集装置还包括贫富液换热器，贫富液换热器具有相连通的富液进口和富液出口以及相连通的贫液进口和贫液出口，富液进口与吸收液出口连通，富液出口与再生进口连通，贫液进口与再生出口连通，贫液出口与吸收液进口连通。
在一些实施例中，二氧化碳捕集装置还包括再沸器，再沸器具有相连通的再沸进口和再沸出口以及相连通的升温进口和升温出口，再沸出口与再生进口连通，再生出口与再沸进口连通，升温进口与热源连通。
应用本公开的技术方案，二氧化碳捕集装置包括脱水塔、吸收组件、再生塔以及加热器，将烟气由脱水塔的脱水进口输送至脱水塔内，利用干燥剂对烟气进行干燥，经干燥后的烟气通过脱水出口和进气口进入至吸收组件内，利用吸收组件内的吸收剂对烟气中的二氧化碳进行吸收并形成富液，去除二氧化碳后的烟气由出气口排出，富液经分相由吸收液出口和再生塔的再生进口进入至再生塔内，富液在再生塔内加热解吸，解吸出的二氧化碳由排气口排出，富液转变为含有吸收剂的贫液，贫液由再生出口和吸收液进口返回至吸收组件内。并且，利用加热器能够对烟气进行加热，加热后的烟气能够由脱水出口进入至脱水塔内，以对吸收水分的干燥剂进行烘干，使干燥剂可以循环利用。由于烟气中的水分利用脱水塔内的干燥剂进行干燥，减少了烟气中的水分含量，从而可以使烟气进入吸收组件后，不会影响系统的水平衡，能够顺利的发生分相。
附图说明
构成本公开的一部分的说明书附图用来提供对本公开的进一步理解，本公开的示意性实施例及其说明用于解释本公开，并不构成对本公开的不当限定。在附图中：
图1示出了根据本公开实施例提供的二氧化碳捕集装置的结构示意图。
其中，上述附图包括以下附图标记：
10、脱水塔；11、关闭阀；20、吸收组件；21、吸收塔；22、分相器；30、再生塔；40、
加热器；50、冷却器；60、分离器；70、预洗塔；80、水洗塔；90、储水槽；100、贫富液换热器；110、再沸器。
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。以下对至少一个示例性实施例的描述实际上仅仅是说明性的，决不作为对本公开及其应用或使用的任何限制。基于本公开中的实施例，本领域普通技术人员在没有作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。
如图1所示，本公开实施例提供了一种二氧化碳捕集装置，二氧化碳捕集装置包括脱水塔10、吸收组件20、再生塔30、加热器40，脱水塔10内设置有干燥烟气的干燥剂，脱水塔10具有相连通的脱水进口和脱水出口，脱水进口与气源连通；吸收组件20具有相连通的进气口和出气口以及相连通的吸收液进口和吸收液出口，进气口与脱水出口连通，出气口与外界连通；再生塔30具有排气口以及相连通的再生进口和再生出口，再生进口与吸收液出口连通，再生出口与吸收液进口连通；加热器40具有加热进口和加热出口，加热进口与气源连通，加热出口与脱水出口连通。
应用本公开的技术方案，二氧化碳捕集装置包括脱水塔10、吸收组件20、再生塔30以及加热器40，将烟气由脱水塔10的脱水进口输送至脱水塔10内，利用干燥剂对烟气进行干燥，经干燥后的烟气通过脱水出口和进气口进入至吸收组件20内，利用吸收组件20内的吸收剂对烟气中的二氧化碳进行吸收并形成富液，去除二氧化碳后的烟气由出气口排出，富液经分相由吸收液出口和再生塔30的再生进口进入至再生塔30内，富液在再生塔30内加热解吸，解吸出的二氧化碳由排气口排出，富液转变为含有吸收剂的贫液，贫液由再生出口和吸收液进口返回至吸收组件20内。并且，利用加热器40能够对烟气进行加热，加热后的烟气能够由脱水出口进入至脱水塔10内，以对吸收水分的干燥剂进行烘干，使干燥剂可以循环利用。由于烟气中的水分利用脱水塔10内的干燥剂进行干燥，减少了烟气中的水分含量，从而可以使烟气进入吸收组件20后，不会影响系统的水平衡，能够顺利的发生分相。
如图1所示，二氧化碳捕集装置还包括冷却器50和分离器60，冷却器50具有相连通的冷却进口和冷却出口，分离器60具有分离进口，冷却进口与脱水进口连通，冷却出口与分离进口连通。再生热吹后烟气由脱水进口进入至冷却器50内，利用冷却器50能够将该高温烟气进行降温，以在分离器60中进行气水的分离。
如图1所示，冷却器50还包括相连通的换热进口和换热出口，换热进口与吸收液出口连通，换热出口与再生进口连通。再生热吹后烟气里含有大量水分，需要对其进行降温以将水分分离。将再生热吹后烟气送入至冷却器50内，利用来自吸收液出口的低温富液(40℃至50℃)对其进行降温，从而将再生热吹烟气中水分分离。同时，来自吸收液出口的低温富液也利用了再生热吹后烟气中的热量，升温后的富液再送入再生塔中进行加热再生，降低了再生能耗。
具体地，再生热吹后烟气由脱水进口和冷却进口进入至冷却器50内，富液由吸收液出口和换热进口进入冷却器50内，烟气对富液进行加热，加热后的富液输送至再生塔30内。
如图1所示，二氧化碳捕集装置还包括预洗塔70，预洗塔70具有预洗冷凝进口以及相连通的烟气进口和烟气出口，烟气进口与气源连通，脱水进口与烟气出口连通，分离器60还具有分离出口以及与分离出口相连通的回流管，回流管的出口与预洗冷凝进口连通。利用预洗塔70能够对含有二氧化碳的烟气进行洗涤，以净化烟气。在分离器60分离后的冷凝水能够通过分离出口、回流管、预洗冷凝进口进入预洗塔70，以为预洗塔70提供水源，使冷凝水进行循环利用。
如图1所示，二氧化碳捕集装置还包括水洗塔80，水洗塔80具有水洗冷凝进口以及相连通的脱碳气进口、脱碳气出口，脱碳气进口与出气口连通，脱碳气出口与外界连通，分离器60还具有分离出口以及与分离出口相连通的回流管，回流管的出口与水洗冷凝进口连通。利用水洗塔80能够对脱碳后的烟气进行洗涤，以使烟气满足排放要求。在分离器60分离后的冷凝水能够通过分离出口、回流管、水洗冷凝进口进入水洗塔80，以为水洗塔80提供水源，使冷凝水进行循环利用。
如图1所示，二氧化碳捕集装置还包括储水槽90，储水槽90设置在回流管上。利用储水槽90能够对分离器60中的冷凝水进行回收和存储，以进一步利用。
如图1所示，脱水塔10为三个，每个脱水塔10的脱水出口分别与加热出口以及进气口连通，每个脱水塔10的脱水进口分别与气源以及冷却进口连通，脱水出口与加热出口的连通管路、脱水出口与进气口的连通管路、脱水进口与气源的连通管路、脱水进口与冷却进口的连通管路上均设置有关闭阀11。通过设置三个脱水塔10，第一个脱水塔10对烟气进行干燥，第二个脱水塔10对吸收水分的干燥剂进行烘干，第三个脱水塔10对烘干后的干燥剂进行降温。以实现脱水塔10的循环工作，使烟气一直能够进行干燥。
具体地，含有二氧化碳的烟气通过脱水进口进入至第一个脱水塔10内，利用第一个脱水塔10内的干燥剂对烟气进行干燥，干燥后的烟气经脱水出口和进气口导入至吸收组件20内进行二氧化碳吸附。同时，含有二氧化碳的烟气经过加热器40加热，加热后的烟气通过脱水出口进入至第二个脱水塔10内，利用该高温烟气对吸收水分的干燥剂进行烘干，烘干后的烟气经脱水进口和冷却进口进入至冷却器50内，富液由吸收液出口和换热进口进入冷却器50内，烟气对富液进行加热。此时，含有二氧化碳的烟气通过脱水进口进入至第三个脱水塔10内，利用该烟气对烘干后的干燥剂进行降温冷却，使干燥剂能够重复利用，降温后的烟气由脱水出口和进气口导入至吸收组件20内进行二氧化碳吸附。
如图1所示，吸收组件20包括相连通的吸收塔21和分相器22，进气口、出气口以及吸收液进口设置于吸收塔21，吸收液出口设置于分相器22。利用吸收塔21能够对烟气中的二氧化碳进行吸收，并进入分相器22中进行分相，并由分相器22进入再生塔30内。
在本实施例中，吸收剂设置在吸收塔21内，吸收二氧化碳后的富液在分相器22内发生分相。
如图1所示，二氧化碳捕集装置还包括贫富液换热器100，贫富液换热器100具有相连通的富液进口和富液出口以及相连通的贫液进口和贫液出口，富液进口与吸收液出口连通，富液出口与再生进口连通，贫液进口与再生出口连通，贫液出口与吸收液进口连通。利用贫富液换热器100，能够使低温的富液和高温的贫液进行换热，以降低系统能耗。
如图1所示，二氧化碳捕集装置还包括再沸器110，再沸器110具有相连通的再沸进口和再沸出口以及相连通的升温进口和升温出口，再沸出口与再生进口连通，再生出口与再沸进口连通，升温进口与热源连通。利用再沸器110能够对再生塔30内的富液进行再次加热，以使二氧化碳能够迅速由富液中析出。
在本实施例中，由于贫液和富液的温度不同，且在吸收塔21内，进气口设置在吸收塔21的下端，出气口设置在吸收塔21的上端，烟气在吸收塔21内上升过程中与吸收剂接触并被吸附，且温度会逐渐降低。在再生塔30内，再生进口设置在再生塔30的上部，再生出口设置在再生塔30的底部，富液在再生塔30中下降，并解析出二氧化碳，且温度会逐渐上升。
需要注意的是，这里所使用的术语仅是为了描述具体实施方式，而非意图限制根据本公开的示例性实施方式。如在这里所使用的，除非上下文另外明确指出，否则单数形式也意图包括复数形式，此外，还应当理解的是，当在本说明书中使用术语“包含”和/或“包括”时，其指明存在特征、步骤、操作、器件、组件和/或它们的组合。
除非另外具体说明，否则在这些实施例中阐述的部件和步骤的相对布置、数字表达式和数值不限制本公开的范围。同时，应当明白，为了便于描述，附图中所示出的各个部分的尺寸并不是按照实际的比例关系绘制的。对于相关领域普通技术人员已知的技术、方法和设备可能不作详细讨论，但在适当情况下，所述技术、方法和设备应当被视为说明书的一部分。在这里示出和讨论的所有示例中，任何具体值应被解释为仅仅是示例性的，而不是作为限制。因此，示例性实施例的其它示例可以具有不同的值。应注意到：相似的标号和字母在下面的附图中表示类似项，因此，一旦某一项在一个附图中被定义，则在随后的附图中不需要对其进行进一步讨论。
在本公开的描述中，需要理解的是，方位词如“前、后、上、下、左、右”、“横向、竖向、垂直、水平”和“顶、底”等所指示的方位或位置关系通常是基于附图所示的方位或位置关系，仅是为了便于描述本公开和简化描述，在未作相反说明的情况下，这些方位词并不指示和暗示所指的装置或元件必须具有特定的方位或者以特定的方位构造和操作，因此不能理解为对本公开保护范围的限制；方位词“内、外”是指相对于各部件本身的轮廓的内外。
为了便于描述，在这里可以使用空间相对术语，如“在……之上”、“在……上方”、“在……上表面”、“上面的”等，用来描述如在图中所示的一个器件或特征与其他器件或特征的空间位置关系。应当理解的是，空间相对术语旨在包含除了器件在图中所描述的方位之外的在使用或操作中的不同方位。例如，如果附图中的器件被倒置，则描述为“在其他器件或构造上方”或“在其他器件或构造之上”的器件之后将被定位为“在其他器件或构造下方”或“在其他器件或构造之下”。因而，示例性术语“在……上方”可以包括“在……上方”和“在……下方”两种方位。该器件也可以其他不同方式定位(旋转90度或处于其他方位)，并且对这里所使用的空间相对描述作出相应解释。
此外，需要说明的是，使用“第一”、“第二”等词语来限定零部件，仅仅是为了便于对相应零部件进行区别，如没有另行声明，上述词语并没有特殊含义，因此不能理解为对本公开保护范围的限制。
以上所述仅为本公开的优选实施例而已，并不用于限制本公开，对于本领域的技术人员来说，本公开可以有各种更改和变化。凡在本公开的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本公开的保护范围之内。

Claims (10)

  1. 一种二氧化碳捕集装置，其中所述二氧化碳捕集装置包括：
    脱水塔(10)，所述脱水塔(10)内设置有干燥烟气的干燥剂，所述脱水塔(10)具有相连通的脱水进口和脱水出口，所述脱水进口与气源连通；
    吸收组件(20)，具有相连通的进气口和出气口以及相连通的吸收液进口和吸收液出口，所述进气口与所述脱水出口连通，所述出气口与外界连通；
    再生塔(30)，具有排气口以及相连通的再生进口和再生出口，所述再生进口与所述吸收液出口连通，所述再生出口与所述吸收液进口连通；
    加热器(40)，具有加热进口和加热出口，所述加热进口与所述气源连通，所述加热出口与所述脱水出口连通。
  2. 根据权利要求1所述的二氧化碳捕集装置，其中所述二氧化碳捕集装置还包括冷却器(50)和分离器(60)，所述冷却器(50)具有相连通的冷却进口和冷却出口，所述分离器(60)具有分离进口，所述冷却进口与所述脱水进口连通，所述冷却出口与分离进口连通。
  3. 根据权利要求2所述的二氧化碳捕集装置，其特征在于，所述冷却器(50)还包括相连通的换热进口和换热出口，所述换热进口与所述吸收液出口连通，所述换热出口与所述再生进口连通。
  4. 根据权利要求2或3所述的二氧化碳捕集装置，其中所述二氧化碳捕集装置还包括预洗塔(70)，所述预洗塔(70)具有预洗冷凝进口以及相连通的烟气进口和烟气出口，所述烟气进口与所述气源连通，所述脱水进口与所述烟气出口连通，所述分离器(60)还具有分离出口以及与所述分离出口相连通的回流管，所述回流管的出口与所述预洗冷凝进口连通。
  5. 根据权利要求2至4中任一项所述的二氧化碳捕集装置，其中所述二氧化碳捕集装置还包括水洗塔(80)，所述水洗塔(80)具有水洗冷凝进口以及相连通的脱碳气进口、脱碳气出口，所述脱碳气进口与所述出气口连通，所述脱碳气出口与外界连通，所述分离器(60)还具有分离出口以及与所述分离出口相连通的回流管，所述回流管的出口与所述水洗冷凝进口连通。
  6. 根据权利要求4或5所述的二氧化碳捕集装置，其特征在于，所述二氧化碳捕集装置还包括储水槽(90)，所述储水槽(90)设置在所述回流管上。
  7. 根据权利要求2至6中任一项所述的二氧化碳捕集装置，其中所述脱水塔(10)为三个，每个所述脱水塔(10)的脱水出口分别与所述加热出口以及所述进气口连通，每个所述脱水塔(10)的脱水进口分别与所述气源以及所述冷却进口连通，所述脱水出口与所述加热出口的连通管路、所述脱水出口与所述进气口的连通管路、所述脱水进口与所述气源的连通管路、所述脱水进口与所述冷却进口的连通管路上均设置有关闭阀(11)。
  8. 根据权利要求1至7中任一项所述的二氧化碳捕集装置，其中所述吸收组件(20)包括相连通的吸收塔(21)和分相器(22)，所述进气口、所述出气口以及所述吸收液进口设置于所述吸收塔(21)，所述吸收液出口设置于所述分相器(22)。
  9. 根据权利要求1至8中任一项所述的二氧化碳捕集装置，其中所述二氧化碳捕集装置还包括贫富液换热器(100)，所述贫富液换热器(100)具有相连通的富液进口和富液出口以及相连通的贫液进口和贫液出口，所述富液进口与所述吸收液出口连通，所述富液出口与所述再生进口连通，所述贫液进口与所述再生出口连通，所述贫液出口与所述吸收液进口连通。
  10. 根据权利要求1至9中任一项所述的二氧化碳捕集装置，其中所述二氧化碳捕集装置还包括再沸器(110)，所述再沸器(110)具有相连通的再沸进口和再沸出口以及相连通的升温进口和升温出口，所述再沸出口与所述再生进口连通，所述再生出口与所述再沸进口连通，所述升温进口与热源连通。
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