WO2024245347A1 - 二氧化碳捕集塔 - Google Patents

二氧化碳捕集塔 Download PDF

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Publication number
WO2024245347A1
WO2024245347A1 PCT/CN2024/096380 CN2024096380W WO2024245347A1 WO 2024245347 A1 WO2024245347 A1 WO 2024245347A1 CN 2024096380 W CN2024096380 W CN 2024096380W WO 2024245347 A1 WO2024245347 A1 WO 2024245347A1
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WO
WIPO (PCT)
Prior art keywords
liquid
washing
section
flue gas
carbon dioxide
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.)
Ceased
Application number
PCT/CN2024/096380
Other languages
English (en)
French (fr)
Inventor
王焕君
郭东方
牛红伟
刘练波
刘牛
范金航
刘汉明
李刚
巩鹏
李百川
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.)
Zhengning Power Plant Of Huaneng Longdong Energy Co Ltd
Huaneng Clean Energy Research Institute
Huaneng Group Technology Innovation Center Co Ltd
Original Assignee
Zhengning Power Plant Of Huaneng Longdong Energy Co Ltd
Huaneng Clean Energy Research Institute
Huaneng Group Technology Innovation Center Co Ltd
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 Zhengning Power Plant Of Huaneng Longdong Energy Co Ltd, Huaneng Clean Energy Research Institute, Huaneng Group Technology Innovation Center Co Ltd filed Critical Zhengning Power Plant Of Huaneng Longdong Energy Co Ltd
Priority to EP24814543.5A priority Critical patent/EP4721841A1/en
Publication of WO2024245347A1 publication Critical patent/WO2024245347A1/zh
Priority to US19/052,323 priority patent/US20250367591A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/12—Washers with plural different washing sections
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/14—Packed scrubbers
    • 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
    • B01D53/1431—Pretreatment by other processes
    • B01D53/145—Pretreatment by separation of solid or liquid material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/185—Liquid distributors
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present application relates to the technical field of carbon dioxide capture, and in particular, to a carbon dioxide capture tower.
  • the basic process flow of flue gas carbon dioxide capture mainly consists of three parts: centered on the absorption tower, supplemented by pre-washing, gas-water separation and boosting equipment; centered on the regeneration tower and reboiler, supplemented by regeneration gas, cooling gas, separator and reflux system; the part between the above two mainly includes carbon dioxide-rich absorption liquid, regeneration absorption liquid heat exchange system and filtration system.
  • the pre-washing process is completed by a specially set pre-washing tower, and a flue gas pipeline is set to connect the pre-washing tower and the absorption tower, and a booster fan is set on the flue gas pipeline to overcome the resistance encountered by the flue gas during transmission.
  • This system in which the pre-washing tower and the absorption tower are set to complete the pre-washing process and the carbon dioxide absorption process respectively, must be equipped with corresponding auxiliary systems for the pre-washing tower and the absorption tower, and flue gas pipelines and booster fans must be added to realize the transmission of flue gas between the pre-washing tower and the absorption tower, which makes the manufacturing cost of the flue gas carbon dioxide capture system high, and the workload of later operation, inspection and maintenance is large; at the same time, the use of a double tower of pre-washing tower and absorption tower occupies a large area and is obviously restricted by the site.
  • the purpose of the present application is to provide a carbon dioxide capture tower in view of at least one technical problem raised in the background technology.
  • One aspect of the present application provides a carbon dioxide capture tower, comprising a pre-wash and impurity removal section, a carbon dioxide absorption section and a flue gas washing section arranged in sequence from bottom to top in a vertical direction, so that the flue gas can flow through the pre-wash and impurity removal section, the carbon dioxide absorption section and the flue gas washing section in sequence, a carbon dioxide capture tower flue gas inlet is provided on the pre-wash and impurity removal section, and a carbon dioxide capture tower flue gas outlet is provided on the washing section.
  • the pre-wash and impurity removal section includes a gas distributor, a first liquid collector, an impurity removal filler, a pre-wash liquid distributor and a pre-wash liquid feed pipe arranged in sequence from bottom to top, and the pre-wash liquid feed pipe is connected to the pre-wash liquid distributor to supply pre-wash liquid for pre-washing flue gas to the pre-wash liquid distributor through the pre-wash liquid feed pipe.
  • the beneficial effect of this technical solution is that after the flue gas enters the pre-wash and impurity removal section through the gas distributor, it can be relatively evenly distributed in the pre-wash and impurity removal section, the pre-wash liquid enters the pre-wash liquid distributor from the pre-wash liquid feed pipe, and is relatively evenly distributed through the pre-wash liquid distributor, the pre-wash liquid is fully in contact with the flue gas in the impurity removal filler, and trace impurities such as gypsum are removed, and the pre-wash liquid that has completed impurity removal falls into the first liquid collector for collection.
  • the carbon dioxide absorption section includes a plurality of segments arranged in a vertical direction, one of the segments is a liquid collection segment, the liquid collection segment is located at the bottom of the segments, the liquid collection segment includes a liquid collector, and the liquid collector includes a mist capture member.
  • the beneficial effect of this technical solution is that by adopting the mist capture element, the lean liquid is effectively prevented from leaking into the pre-washing and impurity removal section.
  • one of the sections is a lean liquid absorption section, which includes a second liquid collector, a first absorption filler, a lean liquid distributor and a lean liquid feed pipe arranged in sequence from bottom to top, the second liquid collector is used for flue gas to pass through, and the lean liquid feed pipe is connected to the lean liquid distributor.
  • the beneficial effect of this technical solution is that the flue gas flows through the second liquid collector and the first absorption filler in the lean liquid absorption section, the lean liquid flows into the lean liquid distributor through the feed pipe, and is evenly sprayed to the first absorption filler.
  • the flue gas and the lean liquid are fully in contact, so that the lean liquid absorbs the carbon dioxide in the flue gas.
  • one of the sections is a cooling absorption section, the liquid collection section, the cooling absorption section and the lean liquid absorption section are arranged in sequence from bottom to top, and the cooling absorption section is used to cool the flue gas and absorb carbon dioxide in the flue gas.
  • the beneficial effect of this technical solution is that in this way, carbon dioxide can be removed from the flue gas in both the cooling absorption section and the lean liquid absorption section, which greatly reduces the carbon dioxide residue that may appear in the flue gas.
  • the lean liquid can also absorb carbon dioxide in the flue gas in the liquid collecting section.
  • the cooling absorption segment includes a third liquid collector, a second absorption filler, an absorption cooling liquid distributor and an absorption cooling liquid feed pipe arranged in sequence from bottom to top, the third liquid collector is used for flue gas to pass through, and the absorption cooling liquid feed pipe is connected to the absorption cooling liquid distributor.
  • the beneficial effect of this technical solution is that in this way, the flue gas is fully in contact with the lean liquid while flowing through the cooling absorption section and the lean liquid absorption section in sequence.
  • the lean liquid absorbs the carbon dioxide in the flue gas and at the same time cools the flue gas, which greatly reduces the carbon dioxide residue that may exist in the flue gas finally discharged from the carbon dioxide capture tower and greatly reduces the temperature of the flue gas before it is discharged from the carbon dioxide capture tower.
  • the flue gas scrubbing section includes a scrubbing section and a defoaming section, and the scrubbing section is located below the defoaming section.
  • the beneficial effect of this technical solution is that by washing the flue gas again, the harmful components that may exist in the flue gas can be reduced to a large extent, making it difficult for these harmful components to be discharged from the carbon dioxide capture tower.
  • the harmful substances in the carbon dioxide capture tower are not easily discharged from the tower in the form of foam.
  • the defoaming segment includes a fourth liquid collector, a first washing filler, a first washing liquid distributor, a first washing liquid feed pipe and a wire mesh defoamer arranged in sequence from bottom to top, the first washing liquid feed pipe is connected to the first washing liquid distributor, and the fourth liquid collector is used for flue gas to pass through.
  • the beneficial effect of this technical solution is that in the defoaming section, the flue gas flows through the fourth liquid collector and the first washing filler in turn, the washing liquid enters the first washing liquid distributor through the first washing liquid feed pipe, and is evenly distributed on the first washing filler.
  • the flue gas In the first washing filler, the flue gas is fully in contact with the washing liquid to absorb the solution components in the flue gas, making it difficult for the solution components to escape with the flue gas and cause losses and secondary pollution.
  • the wire mesh demister makes it difficult for the solution components in the flue gas to flow out of the carbon dioxide capture tower in the form of foam, further reducing the possibility of solution component escape and secondary pollution.
  • the washing section includes a fifth liquid collector, a second washing filler, a second washing liquid distributor and a second washing liquid feed pipe, the second washing liquid distributor is connected to the second washing liquid feed pipe, and the fifth liquid collector is used for allowing flue gas to pass through.
  • the flue gas flows through the fifth liquid collector and the second washing filler in turn, the washing liquid enters the second washing liquid distributor through the second washing liquid feed pipe, and is evenly distributed on the second washing filler.
  • the flue gas is fully in contact with the washing liquid to absorb the solution components in the flue gas, so that the solution is not easy to escape with the flue gas to cause losses and secondary pollution;
  • the flue gas washing section can intercept all the solution components carried by the flue gas.
  • a washing liquid circulation system is also included, and the washing section and the defoaming section are both connected to the washing liquid circulation system.
  • the washing liquid circulation system is used to supply washing liquid to the washing section and the defoaming section, and the washing liquid circulation system is used to receive washing liquid flowing out from the washing section and the defoaming section.
  • the beneficial effect of this technical solution is that the washing liquid can be recycled and reused through the washing liquid circulation system, thus saving costs.
  • the carbon dioxide capture tower provided in the present application arranges the pre-wash impurity removal section, the carbon dioxide absorption section and the flue gas washing section in the same tower, so that the pre-wash process and the carbon dioxide absorption process are carried out in the same tower. Only one set of auxiliary systems is needed for one tower, and the flue gas pipeline and the booster fan previously arranged to connect the pre-wash tower and the absorption tower are removed, thereby reducing the manufacturing cost of the carbon dioxide capture system, making the initial investment of the project lower and reducing the control requirements. At the same time, compared with maintaining the two towers of the pre-wash tower and the absorption tower and the corresponding auxiliary systems, maintaining only the carbon dioxide capture tower and the corresponding auxiliary systems reduces the workload of later operation inspection and maintenance.
  • a carbon dioxide capture system using the carbon dioxide capture tower provided in the embodiment of the present application, the two processes of pre-washing and carbon dioxide absorption can be completed by one tower, which effectively reduces the footprint of the carbon dioxide capture system, making the layout of the carbon dioxide capture system relatively flexible and less restricted by the site; moreover, the use of a pre-washing tower and an absorption tower to complete the two processes of pre-washing and carbon dioxide has poor load adaptability and high energy consumption under low-load conditions, but the carbon dioxide capture tower provided in the present application is easy to operate, has high load adaptability, and has low energy consumption under low-load conditions.
  • FIG1 is a schematic structural diagram of an embodiment of a carbon dioxide capture tower provided in an embodiment of the present application.
  • FIG2 is a partial structural schematic diagram of an embodiment of a carbon dioxide capture tower provided in an example of the present application.
  • FIG3 is a schematic diagram of a liquid collector with a mist capture device provided in an embodiment of the present application.
  • FIG. 4 is a schematic diagram of a liquid collector with a mist capture device provided in an embodiment of the present application.
  • the terms “installed”, “connected”, and “connected” should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components.
  • installed should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components.
  • one aspect of the present application provides a carbon dioxide capture tower, including a pre-wash and impurity removal section 04, a carbon dioxide absorption section 02 and a flue gas washing section 01 arranged in sequence from bottom to top in the vertical direction, so that the flue gas can flow through the pre-wash and impurity removal section 04, the carbon dioxide absorption section 02 and the flue gas washing section 01 in sequence, and a carbon dioxide capture tower flue gas inlet is provided on the pre-wash and impurity removal section 04, and a carbon dioxide capture tower flue gas outlet is provided on the washing section.
  • the flue gas after desulfurization enters the pre-washing and impurity removal section 04 from the flue gas inlet of the carbon dioxide capture tower, flows through the pre-washing and impurity removal section 04, the carbon dioxide absorption section 02 and the flue gas washing section 01 in sequence, and finally flows out of the carbon dioxide capture tower from the flue gas outlet of the carbon dioxide capture tower.
  • the flue gas is pretreated in the pre-washing and impurity removal section 04 to remove trace impurities such as gypsum carried in the flue gas.
  • the flue gas flows from bottom to top in the carbon dioxide absorption section 02 and countercurrently contacts with the lean liquid sprayed into the tower from the top, so that the carbon dioxide is removed.
  • the flue gas enters the flue gas washing section 01, and the solution components carried by the flue gas are recovered by direct spraying water in the flue gas washing section 01, so that the solution is not easy to escape with the flue gas to cause loss and secondary pollution. Finally, the decarbonized flue gas is discharged from the carbon dioxide capture tower.
  • the amine solution that has not absorbed carbon dioxide is called lean liquid, and the amine solution is called rich liquid after absorbing carbon dioxide.
  • the lean liquid can also be called carbon capture absorption solution.
  • the carbon dioxide capture tower provided in the present application arranges the pre-wash impurity removal section 04, the carbon dioxide absorption section 02 and the flue gas washing section 01 in the same tower, so that the pre-wash process and the carbon dioxide absorption process are carried out in the same tower.
  • the carbon dioxide capture system using the carbon dioxide capture tower provided in the embodiment of the present application can complete the two processes of pre-washing and carbon dioxide absorption with one tower, which effectively reduces the footprint of the carbon dioxide capture system, making the layout of the carbon dioxide capture system relatively flexible and less restricted by the site; moreover, the use of
  • the pre-washing and impurity removal section 04 includes a gas distributor 13, a first liquid collector 12, an impurity removal filler 10, a pre-washing liquid distributor 03 and a pre-washing liquid feed pipe 16 arranged in sequence from bottom to top, and the pre-washing liquid feed pipe 16 is connected to the pre-washing liquid distributor 03 to supply pre-washing liquid for pre-washing flue gas to the pre-washing liquid distributor 03 through the pre-washing liquid feed pipe 16.
  • the pre-washing liquid distributor 03 After the flue gas enters the pre-washing and impurity removal section 04 through the gas distributor 13, it can be relatively evenly distributed in the pre-washing and impurity removal section 04, and the pre-washing liquid enters the pre-washing liquid distributor 03 from the pre-washing liquid feed pipe 16 and is relatively evenly distributed through the pre-washing liquid distributor 03.
  • the pre-washing liquid fully contacts the flue gas in the impurity removal filler 10 to remove trace impurities such as gypsum, and the pre-washing liquid that has completed impurity removal falls into the first liquid collector 12 for collection;
  • the pre-washing liquid distributor 03 is preferably a liquid spraying device.
  • the carbon dioxide absorption section 02 includes a plurality of sections arranged in the vertical direction, one of the sections is a liquid collection section, and the liquid collection section is located at the bottom of the sections.
  • the liquid collection section includes a liquid collector 09, and the liquid collector 09 includes a mist capture piece.
  • the mist capture piece described in the embodiment of the present application is a mist capture piece or other mist capture device; by adopting the mist capture piece, the lean liquid is effectively prevented from leaking into the pre-washing and impurity removal section 04.
  • the liquid collection section also includes an absorption filler 17, and the absorption filler 17 is arranged above the liquid collector 09.
  • the flue gas in the liquid collection section flows through the liquid collector 09 and the absorption filler 17 in sequence.
  • the lean liquid flowing into the liquid collection section from above is fully in contact with the flue gas in the absorption filler 17, so that the lean liquid can absorb the carbon dioxide in the flue gas.
  • a liquid collector with a mist capture device provided in an embodiment of the present application includes a bottom plate 1, an air riser 2, and an air riser cap 3.
  • the air riser cap includes a top plate and a flange 5, and the flange 5 of the air riser cap is downward, and the mist capture device 4 is arranged in the space formed between the air riser and the flange of the air riser cap 5.
  • the present invention prevents the liquid above and below the liquid collector from being mixed back by arranging the mist capture device 4 between the air riser 2 and the flange 5 of the air riser cap.
  • one of the sections is a lean liquid absorption section
  • the lean liquid absorption section includes a second liquid collector 06, a first absorption filler 20, a lean liquid distributor 21 and a lean liquid feed pipe 26 arranged in sequence from bottom to top, the second liquid collector 06 is used for flue gas to pass through, and the lean liquid feed pipe 26 is connected to the lean liquid distributor 21.
  • the lean liquid absorption section and the liquid collection section are not the same section;
  • the second liquid collector 06 is preferably a gas cap liquid collector;
  • the flue gas flows through the second liquid collector 06 and the first absorption filler 20 in the lean liquid absorption section, and the lean liquid flows into the lean liquid distributor 21 through the feed pipe and is evenly sprayed to the first absorption filler 20, in which the flue gas is fully in contact with the lean liquid, so that the lean liquid absorbs carbon dioxide in the flue gas;
  • the lean liquid distributor 21 is preferably a liquid spraying device.
  • one of the sections is a cooling absorption section
  • the liquid collection section, the cooling absorption section and the lean liquid absorption section are arranged in sequence from bottom to top, and the cooling absorption section is used to cool the flue gas and absorb carbon dioxide in the flue gas.
  • the flue gas can achieve carbon dioxide removal in both the cooling absorption section and the lean liquid absorption section, which greatly reduces the carbon dioxide residue that may appear in the flue gas.
  • the absorption filler 17 is provided in the liquid collection section, the lean liquid can also absorb carbon dioxide in the flue gas in the liquid collection section.
  • the cooling absorption section includes a third collector 08, a second absorption filler 18, an absorption coolant distributor 07 and an absorption coolant feed pipe 19 arranged in sequence from bottom to top, the third collector 08 is used for flue gas to pass through, and the absorption coolant feed pipe 19 is connected to the absorption coolant distributor 07.
  • the third collector 08 is used for flue gas to pass through
  • the absorption coolant feed pipe 19 is connected to the absorption coolant distributor 07.
  • the third collector 08 is preferably a gas cap collector; the absorption coolant distributor 07 is preferably a liquid spraying device.
  • the flue gas scrubbing section 01 includes a scrubbing section and a defoaming section, and the scrubbing section is located below the defoaming section.
  • the flue gas is scrubbed again to reduce the harmful components that may exist in the flue gas to a large extent, so that these harmful components are not easily discharged from the carbon dioxide capture tower.
  • the defoaming section is provided to prevent the harmful substances in the carbon dioxide capture tower from being easily discharged from the tower in the form of foam.
  • the defoaming segment includes a fourth liquid collector 27, a first washing filler 28, a first washing liquid distributor 23, a first washing liquid feed pipe 24 and a wire mesh defoamer 25 arranged in sequence from bottom to top, the first washing liquid feed pipe 24 is connected to the first washing liquid distributor 23, and the fourth liquid collector 27 is used for flue gas to pass through.
  • the fourth liquid collector 27 is preferably a gas lift cap liquid collector
  • the first washing liquid distributor 23 is preferably a liquid spraying device. In the defoaming section, the flue gas flows through the fourth liquid collector 27 and the first washing filler 28 in sequence.
  • the washing liquid enters the first washing liquid distributor 23 through the first washing liquid feed pipe 24 and is evenly distributed on the first washing filler 28.
  • the flue gas is fully in contact with the washing liquid to absorb the solution components in the flue gas, so that the solution components are not easy to escape with the flue gas to cause loss and secondary pollution.
  • the wire mesh demister 25 makes it difficult for the solution components in the flue gas to flow out of the carbon dioxide capture tower in the form of foam, further reducing the possibility of solution component escape and secondary pollution.
  • the washing segment includes a fifth liquid collector 29, a second washing filler 30, a second washing liquid distributor 05 and a second washing liquid feed pipe 22, wherein the second washing liquid distributor 05 is connected to the second washing liquid feed pipe 22, and the fifth liquid collector 29 is used for flue gas to pass through.
  • the fifth liquid collector 29 is preferably a gas lift cap liquid collector
  • the second washing liquid distributor 05 is preferably a liquid spraying device.
  • the flue gas flows through the fifth liquid collector 29 and the second washing filler 30 in turn, and the washing liquid enters the second washing liquid distributor 05 through the second washing liquid feed pipe 22 and is evenly distributed on the second washing filler 30.
  • the flue gas is fully in contact with the washing liquid to absorb the solution components in the flue gas, so that the solution is not easy to escape with the flue gas to cause loss and secondary pollution; through the two washing and one defoaming of the flue gas by the washing section and the defoaming section, a triple interception is formed for the solution components that may be carried by the flue gas, making it more difficult for the solution components to escape with the flue gas.
  • the flue gas washing section 01 can intercept all the solution components carried by the flue gas.
  • the carbon dioxide capture tower provided in the embodiment of the present application further includes a washing liquid circulation system, the washing segment and the defoaming segment are both connected to the washing liquid circulation system, the washing liquid circulation system is used to supply washing liquid to the washing segment and the defoaming segment, and the washing liquid circulation system is used to receive the washing liquid flowing out from the washing segment and the defoaming segment.
  • the washing liquid circulation system has a water replenishment function, and when washing liquid is lost, desalted water can be supplemented as washing liquid.
  • each filler in the embodiment of the present application is provided with an auxiliary component for supporting and fixing the filler
  • the auxiliary component may include a support beam 11, a support grid 14, a pressing plate 15, etc.
  • the pre-washing impurity removal section 04 also includes a support beam 11, a support grid 14, and a pressing plate 15, and the gas distributor 13, the first liquid collector 12, the support beam 11, the support grid 14, the impurity removal filler 10, the pressing plate 15, the pre-washing liquid distributor 03 and the pre-washing liquid feed pipe 16 are arranged in sequence from bottom to top, the support beam 11 and the support grid 14 are used to support the impurity removal filler 10, and the pressing plate 15 is used to press the impurity removal filler 10.
  • the filler used in the flue gas washing section 01 and the pre-washing impurity removal section 04 is preferably PP (Chinese name is polypropylene) material
  • the filler used in the carbon dioxide absorption section 02 is preferably 304 stainless steel, such as 304 stainless steel regular corrugated filler, 304 stainless steel regular filler or 304 metal honeycomb inclined plate filler.
  • the pre-washing liquid is preferably a low-concentration sodium hydroxide aqueous solution, that is, alkaline solution.
  • the present application also provides an application example of the carbon dioxide capture tower, in which the pre-washing and impurity removal section 04 is also called the pre-washing section, the carbon dioxide absorption section 02 is also called the absorption section, the flue gas washing section 01 is also called the washing section, the support beam 11 is also called the packing support beam, and the carbon dioxide capture tower is also called the composite absorption tower.
  • the application example is as follows:
  • This application example involves a new type of composite absorption tower for carbon dioxide capture, which has the functions of a pre-wash tower and an absorption tower in the traditional process, that is, the flue gas is washed, cooled, and CO2 is recovered in the CO2 composite absorption tower, and then discharged from the top of the CO2 composite absorption tower after further washing and cooling.
  • the basic process flow of flue gas CO2 capture mainly consists of three parts: centered on the absorption tower, supplemented by pre-washing, gas-water separation and boosting equipment; centered on the regeneration tower and reboiler, supplemented by regeneration gas, cooling gas, separator and reflux system; the part between the above two mainly includes CO2-rich absorption liquid, regeneration absorption liquid heat exchange system and filtration system.
  • the flue gas temperature at the outlet is about 48°C, which is the ideal absorption temperature range for amine solution.
  • the flue gas is pretreated in the pre-wash tower to remove trace impurities such as gypsum carried by the flue gas.
  • a booster fan is used to overcome the resistance of the gas passing through the pre-treatment system and the absorption tower.
  • the flue gas flows from bottom to top and contacts the amine solution sprayed into the tower from the top in countercurrent, so that CO2 is removed and the tail gas is discharged into the atmosphere from the top of the tower.
  • a tail gas washing section is set at the top of the absorption tower to recover the solution components carried by the flue gas through direct spraying and washing. The washing water is recycled.
  • the washing water is first used as the system water, and the lost washing water is supplemented by desalted water.
  • the rich liquid after absorbing CO2 is pumped from the bottom of the tower into the lean-rich liquid heat exchanger, sprayed into the upper part of the regeneration tower, and partially desorbed by steam stripping.
  • the semi-lean liquid after steam stripping desorption enters the reboiler to further desorb CO2.
  • the lean liquid after CO2 desorption in the reboiler flows out from the bottom of the regeneration tower, and after being cooled by the lean-rich liquid heat exchanger and the lean liquid cooler, it enters the absorption tower for recycling.
  • the back-and-forth circulation of the solvent constitutes a process of continuous absorption and desorption of CO2.
  • the desorbed CO2 and water vapor are cooled, separated and dehydrated to obtain high-purity CO2 gas, which is then sent to the subsequent compression system.
  • the condensed water separated from the regenerated gas is pumped to the regeneration tower to adjust the temperature inside the regeneration tower.
  • a solution purification and recovery system is set up. When necessary, part of the lean solution is sent to the purification and recovery system and a specified alkali solution is added for purification and recovery.
  • the pre-wash tower and the absorption tower are set separately, which has the following problems: 1)
  • the double towers and their relatively complete auxiliary system configuration make the system process relatively complex, with high control requirements, high initial project investment, and a large workload for later operation, inspection and maintenance; 2) Due to the installation of two towers, the floor area is larger than that of a single tower, and the application is obviously restricted by the site; 3) The load adaptability is poor, and the energy consumption is high under low load conditions.
  • the composite absorption tower proposed in this application example combines the pre-washing tower and the absorption tower into one.
  • the flue gas from the unit desulfurization system first enters the pre-washing section of the composite absorption tower to pre-treat the flue gas and remove trace impurities such as gypsum carried by the flue gas; then enters the absorption section of the composite absorption tower for decarbonization; finally, the flue gas enters the washing section to recover the solution components carried by the flue gas. That is, the flue gas is washed, cooled, and CO2 is recovered in the CO2 composite absorption tower, and then discharged from the top of the CO2 composite absorption tower after washing and cooling.
  • the advantages of the composite absorption tower are: 1) The double towers are combined into one, the carbon capture system process is relatively simple, the initial investment of the project is low, and the workload of later operation inspection and maintenance is small; 2) The floor area is smaller than that of a single tower, and the application is less restricted by the site; 3) It is easy to operate, has a high adaptability to load, and has low energy consumption under low load conditions.
  • the composite absorption tower includes a pre-washing section, an absorption section and a washing section from bottom to top.
  • the flue gas enters the composite absorption tower from the bottom of the tower.
  • the functions of each section are as follows:
  • the flue gas is pretreated to remove trace impurities such as gypsum carried by the flue gas.
  • the flue gas flows from bottom to top and countercurrently contacts the carbon capture absorption solution sprayed into the tower from the top, so that CO2 is removed and the tail gas enters the scrubbing section.
  • a liquid collector with a mist capture device is installed in the pre-wash section and the absorption section to prevent the capture solution from leaking into the pre-wash section.
  • the solution components carried by the flue gas are recovered by direct spraying and washing, so as to avoid the loss and secondary pollution caused by the escape of the solution with the flue gas.
  • the washing water can be recycled.
  • the washing water is first used to replenish the system, and the lost washing water is replenished with desalted water.
  • Pre-wash section (Bed6), the structural layout from bottom to top should be gas distributor, liquid collector, packing support beam, support grid, packing, pressure plate, liquid distributor, feed pipe;
  • Tail gas washing section (Bed1-2): the structural layout of Bed2 should be liquid collector, filler and its accessories, liquid distributor, lower washing liquid feed pipe; the structural layout of Bed1 should be liquid collector, filler and its accessories, liquid distributor, upper washing liquid feed pipe, wire mesh demister and its accessories.
  • the composite absorption tower proposed in this application example combines the pre-washing tower and the absorption tower into one.
  • the flue gas from the unit desulfurization system first enters the pre-washing section of the composite absorption tower to pre-treat the flue gas and remove trace impurities such as gypsum carried by the flue gas; then enters the absorption tower for decarbonization; finally, the flue gas enters the washing section to recover the solution components carried by the flue gas. That is, the flue gas is washed, cooled, and CO2 is recovered in the CO2 composite absorption tower, and then discharged from the top of the CO2 composite absorption tower after washing and cooling.
  • the advantages of the composite absorption tower are: 1) The double towers are combined into one, the carbon capture system process is relatively simple, the initial investment of the project is low, and the workload of later operation inspection and maintenance is small; 2) The floor area is smaller than that of a single tower, and the application is less restricted by the site; 3) It is easy to operate, has a high adaptability to load, and has low energy consumption under low load conditions.

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Abstract

一种二氧化碳捕集塔，包括在竖直方向上从下到上依次排列的预洗除杂段（04）、二氧化碳吸收段（02）和烟气洗涤段（01），以使烟气能够依次流经预洗除杂段（04）、二氧化碳吸收段（02）和烟气洗涤段（01），在预洗除杂段（04）上设置有二氧化碳捕集塔烟气入口，在烟气洗涤段（01）上设置有二氧化碳捕集塔烟气出口。

Description

二氧化碳捕集塔 技术领域
本申请涉及二氧化碳捕集技术领域，具体而言，涉及一种二氧化碳捕集塔。
 背景技术
烟气二氧化碳捕集的基本工艺流程主要由三部分组成：以吸收塔为中心，辅以预洗、气水分离及增压设备；以再生塔和再沸器为中心，辅以再生气、冷却气以及分离器和回流系统；介于以上两者之间的部分，主要有富二氧化碳吸收液、再生吸收液换热系统以及过滤系统。其中的预洗工序由专门设置的预洗塔完成，设置烟气管路连接预洗塔和吸收塔，并在烟气管路上设置了增压风机以克服烟气在传输时所遇到的阻力。这种设置预洗塔和吸收塔分别完成预洗工序和二氧化碳吸收工序的系统，必须为预洗塔和吸收塔分别配置相应的辅助系统，并且必须增设烟气管路和增压风机实现烟气在预洗塔和吸收塔之间传输，这使得烟气二氧化碳捕集系统制造成本较高，且后期运行检修维护工作量较大；同时，采用预洗塔和吸收塔双塔设置占地面积较大，受场地制约较明显。
 发明内容
本申请的目的在于针对背景技术中所提出的至少一个技术问题，提供一种二氧化碳捕集塔。
为了实现上述目的，本申请采用以下技术方案：
本申请的一个方面提供一种二氧化碳捕集塔，包括在竖直方向上从下到上依次排列的预洗除杂段、二氧化碳吸收段和烟气洗涤段，以使烟气能够依次流经预洗除杂段、二氧化碳吸收段和烟气洗涤段，在所述预洗除杂段上设置有二氧化碳捕集塔烟气入口，在所述洗涤段上设置有二氧化碳捕集塔烟气出口。
可选地，所述预洗除杂段包括从下到上依次排列的气体分布器、第一集液器、除杂填料、预洗液分布器和预洗液进料管，所述预洗液进料管与所述预洗液分布器连通以通过所述预洗液进料管向所述预洗液分布器供给用于预洗烟气的预洗液。
该技术方案的有益效果在于：通过气体分布器使烟气进入预洗除杂段后能够在预洗除杂段中相对均匀的分布，预洗液从预洗液进料管进入预洗液分布器，并通过预洗液分布器相对均匀的分布，在除杂填料中预洗液与烟气充分接触，实现对微量石膏等杂质的清除，完成除杂的预洗液落入第一集液器中进行收集。
可选地，所述二氧化碳吸收段包括在竖直方向上排列的多个分段，各所述分段之一为集液分段，在各所述分段中所述集液分段位于最下方，所述集液分段包括液体收集器，所述液体收集器包括雾沫捕集件。
该技术方案的有益效果在于：通过采用雾沫捕集件，有效防止贫液漏液到预洗除杂段。
可选地，各所述分段之一为贫液吸收分段，所述贫液吸收分段包括从下到上依次排列的第二集液器、第一吸收填料、贫液分布器和贫液进料管，所述第二集液器用于供烟气通过，所述贫液进料管与所述贫液分布器连通。
该技术方案的有益效果在于：烟气在贫液吸收分段中流经第二集液器和第一吸收填料，贫液通过进料管流入贫液分布器，均匀的喷淋到第一吸收填料，在第一吸收填料中烟气与贫液充分接触，使贫液吸收烟气中的二氧化碳。
可选地，各所述分段之一为冷却吸收分段，所述集液分段、所述冷却吸收分段和所述贫液吸收分段从下到上依次排列，所述冷却吸收分段用于冷却烟气并吸收烟气中的二氧化碳。
该技术方案的有益效果在于：这样，相当于烟气在冷却吸收分段和贫液吸收分段中均能够实现二氧化碳清除，较大程度的减少了烟气中可能出现的二氧化碳残留，当集液分段中设置吸收填料时，贫液在集液分段中也能够吸收烟气中的二氧化碳。
可选地，所述冷却吸收分段包括从下到上依次排列的第三集液器、第二吸收填料、吸收冷却液分布器和吸收冷却液进料管，所述第三集液器用于供烟气通过，所述吸收冷却液进料管与所述吸收冷却液分布器连通。
该技术方案的有益效果在于：这样，烟气在依次流过冷却吸收分段和贫液吸收分段的过程中，均与贫液充分接触，贫液吸收烟气中的二氧化碳，同时贫液也对烟气进行冷却，这较大程度的减少了最后排出二氧化碳捕集塔的烟气中可能存在的二氧化碳残留，并在排出二氧化碳捕集塔之前较大程度的降低了烟气的温度。
可选地，所述烟气洗涤段包括洗涤分段和除沫分段，所述洗涤分段位于所述除沫分段的下方。
该技术方案的有益效果在于：对烟气再次洗涤，可较大限度的减小烟气中可能存在的有害成分，使这些有害成分不易从二氧化碳捕集塔中被排出，设置除沫分段，则使二氧化碳捕集塔中的有害物质不易以泡沫的形式从塔中排出。
可选地，所述除沫分段包括从下到上依次排列的第四集液器、第一洗涤填料、第一洗涤液分布器、第一洗涤液进料管和丝网除沫器，所述第一洗涤液进料管与所述第一洗涤液分布器连通，所述第四集液器用于供烟气通过。
该技术方案的有益效果在于：在除沫分段中烟气依次流经第四集液器和第一洗涤填料，洗涤液通过第一洗涤液进料管进入第一洗涤液分布器，较均匀的分布在第一洗涤填料上，在第一洗涤填料中，烟气与洗涤液充分接触以吸收烟气中的溶液成分，使溶液成分不易随烟气逃逸造成损失及二次污染，丝网除沫器则使烟气中的溶液成分不易以泡沫形式从二氧化碳捕集塔流出，进一步降低溶液成分逃逸及二次污染的可能。
可选地，所述洗涤分段包括第五集液器、第二洗涤填料、第二洗涤液分布器和第二洗涤液进料管，所述第二洗涤液分布器与第二洗涤液进料管连通，所述第五集液器用于供烟气通过。
该技术方案的有益效果在于：在洗涤分段中烟气依次流经第五集液器和第二洗涤填料，洗涤液通过第二洗涤液进料管进入第二洗涤液分布器，并较均匀的分布在第二洗涤填料上，在第二洗涤填料中，烟气与洗涤液充分接触以吸收烟气中的溶液成分，使溶液不易随烟气逃逸造成损失及二次污染；通过洗涤分段和除沫分段对烟气的两次洗涤和一次除沫，对烟气可能挟带的溶液成分形成三重拦截，使溶液成分较难随烟气逃逸，在一些较理想的情况下，烟气洗涤段机会可以拦截烟气中挟带的全部溶液成分。
可选地，还包括洗涤液循环系统，所述洗涤分段和所述除沫分段均与所述洗涤液循环系统连接，所述洗涤液循环系统用于向所述洗涤分段和所述除沫分段供给洗涤液，且所述洗涤液循环系统用于接收从所述洗涤分段和所述除沫分段流出的洗涤液。
该技术方案的有益效果在于：这样，通过洗涤液循环系统可以对洗涤液进行循环再利用，节省成本。
本申请提供的技术方案可以达到以下有益效果：
本申请所提供的二氧化碳捕集塔，通过将预洗除杂段、二氧化碳吸收段和烟气洗涤段设置在同一个塔，使预洗工序和二氧化碳吸收工序在同一个塔内进行，一个塔只需要一套辅助系统，并且去掉了过去为连接预洗塔和吸收塔而设置的烟气管路和增压风机，因此降低了二氧化碳捕集系统的制造成本，使得项目初期投资较低，控制要求也有所降低；同时，相对于维护预洗塔和吸收塔这两个塔及相应的辅助系统，仅维护二氧化碳捕集塔这一个塔及相应的辅助系统减少了后期运行检修维护的工作量；另外，相对于传统的采用预洗塔和吸收塔这两个塔完成预洗和二氧化碳吸收这两个工序的二氧化碳捕集系统，应用了本申请实施例所提供的二氧化碳捕集塔的二氧化碳捕集系统，预洗和二氧化碳吸收这两个工序一个塔即可完成，有效减小了二氧化碳捕集系统的占地面积，使得二氧化碳捕集系统的布置方式相对较灵活，受场地限制较小；而且，采用预洗塔和吸收塔这两个塔完成预洗和二氧化碳这两个工序，对负荷适应性较差，低负荷工况下能耗较高，但采用本申请所提供的二氧化碳捕集塔操作方便，对负荷适应性较高，低负荷工况下能耗较低。
为让本发明的上述和其他目的、特征和优点能更明显易懂，下文特举较佳实施例，并配合所附图式，作详细说明如下。
 附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。
图1为本申请实施例提供的二氧化碳捕集塔的一种实施方式的结构示意图；
图2为本申请实施例提供的二氧化碳捕集塔的一种实施方式的部分结构示意图；
图3为本申请实施例提供的带有雾沫捕集装置的液体收集器的示意图；
图4为本申请实施例提供的带有雾沫捕集装置的液体收集器的示意图。
附图标记：
01-烟气洗涤段；                    02-二氧化碳吸收段；
03-预洗液分布器；                  04-预洗除杂段；
05-第二洗涤液分布器；              06-第二集液器；
07-吸收冷却液分布器；              08-第三集液器；
09-液体收集器；                    10-除杂填料；
11-支撑梁；                        12-第一集液器；
13-气体分布器；                    14-支撑格栅；
15-压板；                          16-预洗液进料管；
17-吸收填料；                      18-第二吸收填料；
19-吸收冷却液进料管；              20-第一吸收填料；
21-贫液分布器；                    22-第二洗涤液进料管；
23-第一洗涤液分布器；              24-第一洗涤液进料管；
25-丝网除沫器；                    26-贫液进料管；
27-第四集液器；                    28-第一洗涤填料；
29-第五集液器；                    30-第二洗涤填料；
1-底板；                           2-升气管；
3-升气帽；                         5-翻边；
4-雾沫捕集装置。
 具体实施方式
下面将结合附图对本申请的技术方案进行清楚、完整地描述，显然，所描述的实施例是本申请一部分实施例，而不是全部的实施例。基于本申请中的实施例，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，都属于本申请保护的范围。
在本申请的描述中，需要说明的是，术语“中心”、“上”、“下”、“左”、“右”、“竖直”、“水平”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本申请和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本申请的限制。此外，术语“第一”、“第二”、“第三”仅用于描述目的，而不能理解为指示或暗示相对重要性。
在本申请的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本申请中的具体含义。
如图1和图2所示，本申请的一个方面提供一种二氧化碳捕集塔，包括在竖直方向上从下到上依次排列的预洗除杂段04、二氧化碳吸收段02和烟气洗涤段01，以使烟气能够依次流经预洗除杂段04、二氧化碳吸收段02和烟气洗涤段01，在所述预洗除杂段04上设置有二氧化碳捕集塔烟气入口，在所述洗涤段上设置有二氧化碳捕集塔烟气出口。
在使用时，来自脱硫后的烟气从二氧化碳捕集塔烟气入口进入预洗除杂段04，依次流经预洗除杂段04、二氧化碳吸收段02和烟气洗涤段01，最后从二氧化碳捕集塔烟气出口流出二氧化碳捕集塔，在预洗除杂段04中对烟气进行预处理，除去烟气中挟带的微量石膏等杂质，烟气在二氧化碳吸收段02中自下向上流动，与从上部喷淋入塔的贫液逆流接触，使二氧化碳得到脱除，烟气进入烟气洗涤段01，在烟气洗涤段01通过直接喷淋水洗，回收烟气携带的溶液成分，使溶液不易随烟气的逃逸造成损失及二次污染，最后从二氧化碳捕集塔排出的是脱碳烟气。本申请实施例中，将尚未吸收二氧化碳的胺溶液称为贫液，胺溶液吸收二氧化碳之后称为富液，贫液也可称为碳捕集吸收溶液。
本申请所提供的二氧化碳捕集塔，通过将预洗除杂段04、二氧化碳吸收段02和烟气洗涤段01设置在同一个塔，使预洗工序和二氧化碳吸收工序在同一个塔内进行，一个塔只需要一套辅助系统(包括但不限于底部支撑系统)，并且去掉了过去为连接预洗塔和吸收塔而设置的烟气管路和增压风机，因此降低了二氧化碳捕集系统的制造成本，使得项目初期投资较低，控制要求也有所降低；同时，相对于维护预洗塔和吸收塔这两个塔及相应的辅助系统，仅维护二氧化碳捕集塔这一个塔及相应的辅助系统减少了后期运行检修维护的工作量；另外，相对于传统的采用预洗塔和吸收塔这两个塔完成预洗和二氧化碳吸收这两个工序的二氧化碳捕集系统，应用了本申请实施例所提供的二氧化碳捕集塔的二氧化碳捕集系统，预洗和二氧化碳吸收这两个工序一个塔即可完成，有效减小了二氧化碳捕集系统的占地面积，使得二氧化碳捕集系统的布置方式相对较灵活，受场地限制较小；而且，采用预洗塔和吸收塔这两个塔完成预洗和二氧化碳这两个工序，对负荷适应性较差，低负荷工况下能耗较高，但采用本申请所提供的二氧化碳捕集塔操作方便，对负荷适应性较高，低负荷工况下能耗较低。
可选地，所述预洗除杂段04包括从下到上依次排列的气体分布器13、第一集液器12、除杂填料10、预洗液分布器03和预洗液进料管16，所述预洗液进料管16与所述预洗液分布器03连通以通过所述预洗液进料管16向所述预洗液分布器03供给用于预洗烟气的预洗液。通过气体分布器13使烟气进入预洗除杂段04后能够在预洗除杂段04中相对均匀的分布，预洗液从预洗液进料管16进入预洗液分布器03，并通过预洗液分布器03相对均匀的分布，在除杂填料10中预洗液与烟气充分接触，实现对微量石膏等杂质的清除，完成除杂的预洗液落入第一集液器12中进行收集；预洗液分布器03优选为液体喷淋设备。
可选地，所述二氧化碳吸收段02包括在竖直方向上排列的多个分段，各所述分段之一为集液分段，在各所述分段中所述集液分段位于最下方，所述集液分段包括液体收集器09，所述液体收集器09包括雾沫捕集件。本申请实施例中所述的雾沫捕集件为雾沫捕集器或其他雾沫捕集装置；通过采用雾沫捕集件，有效防止贫液漏液到预洗除杂段04。优选的，集液分段还包括吸收填料17，吸收填料17设置在液体收集器09的上方，集液分段中的烟气依次流过液体收集器09和吸收填料17，从上方流入集液分段的贫液在吸收填料17中与烟气充分接触，使贫液能够吸收烟气中的二氧化碳。
如图3、图4所示，为本申请一实施例提供的带有雾沫捕集装置的液体收集器，包含底板1，升气管2，升气帽3，升气帽含顶板和翻边5，并且升气帽的翻边5向下，雾沫捕集装置4设置于升气管和升气帽5翻边之间形成的空间。
本发明通过在升气管2和升气帽翻边5之间设置雾沫捕集装置4，防止了液体收集器上方和下方的液体返混。
可选地，各所述分段之一为贫液吸收分段，所述贫液吸收分段包括从下到上依次排列的第二集液器06、第一吸收填料20、贫液分布器21和贫液进料管26，所述第二集液器06用于供烟气通过，所述贫液进料管26与所述贫液分布器21连通。可以理解的，贫液吸收分段与集液分段并非同一个分段；第二集液器06优选为升气帽集液器；烟气在贫液吸收分段中流经第二集液器06和第一吸收填料20，贫液通过进料管流入贫液分布器21，均匀的喷淋到第一吸收填料20，在第一吸收填料20中烟气与贫液充分接触，使贫液吸收烟气中的二氧化碳；贫液分布器21优选为液体喷淋设备。
可选地，各所述分段之一为冷却吸收分段，所述集液分段、所述冷却吸收分段和所述贫液吸收分段从下到上依次排列，所述冷却吸收分段用于冷却烟气并吸收烟气中的二氧化碳。这样，相当于烟气在冷却吸收分段和贫液吸收分段中均能够实现二氧化碳清除，较大程度的减少了烟气中可能出现的二氧化碳残留，当集液分段中设置吸收填料17时，贫液在集液分段中也能够吸收烟气中的二氧化碳。
可选地，所述冷却吸收分段包括从下到上依次排列的第三集液器08、第二吸收填料18、吸收冷却液分布器07和吸收冷却液进料管19，所述第三集液器08用于供烟气通过，所述吸收冷却液进料管19与所述吸收冷却液分布器07连通。本申请实施例中，优选的采用同样作为贫液的胺溶液作为吸收冷却液，这样，烟气在依次流过冷却吸收分段和贫液吸收分段的过程中，均与贫液充分接触，贫液吸收烟气中的二氧化碳，同时贫液也对烟气进行冷却，这较大程度的减少了最后排出二氧化碳捕集塔的烟气中可能存在的二氧化碳残留，并在排出二氧化碳捕集塔之前较大程度的降低了烟气的温度。第三集液器08优选为升气帽集液器；吸收冷却液分布器07优选为液体喷淋设备。
可选地，所述烟气洗涤段01包括洗涤分段和除沫分段，所述洗涤分段位于所述除沫分段的下方。对烟气再次洗涤，可较大限度的减小烟气中可能存在的有害成分，使这些有害成分不易从二氧化碳捕集塔中被排出，设置除沫分段，则使二氧化碳捕集塔中的有害物质不易以泡沫的形式从塔中排出。
可选地，所述除沫分段包括从下到上依次排列的第四集液器27、第一洗涤填料28、第一洗涤液分布器23、第一洗涤液进料管24和丝网除沫器25，所述第一洗涤液进料管24与所述第一洗涤液分布器23连通，所述第四集液器27用于供烟气通过。本申请实施例中，第四集液器27优选为升气帽集液器，第一洗涤液分布器23优选为液体喷淋设备。在除沫分段中烟气依次流经第四集液器27和第一洗涤填料28，洗涤液通过第一洗涤液进料管24进入第一洗涤液分布器23，较均匀的分布在第一洗涤填料28上，在第一洗涤填料28中，烟气与洗涤液充分接触以吸收烟气中的溶液成分，使溶液成分不易随烟气逃逸造成损失及二次污染，丝网除沫器25则使烟气中的溶液成分不易以泡沫形式从二氧化碳捕集塔流出，进一步降低溶液成分逃逸及二次污染的可能。
可选地，所述洗涤分段包括第五集液器29、第二洗涤填料30、第二洗涤液分布器05和第二洗涤液进料管22，所述第二洗涤液分布器05与第二洗涤液进料管22连通，所述第五集液器29用于供烟气通过。本申请实施例中，第五集液器29优选为升气帽集液器，第二洗涤液分布器05优选为液体喷淋设备。在洗涤分段中烟气依次流经第五集液器29和第二洗涤填料30，洗涤液通过第二洗涤液进料管22进入第二洗涤液分布器05，并较均匀的分布在第二洗涤填料30上，在第二洗涤填料30中，烟气与洗涤液充分接触以吸收烟气中的溶液成分，使溶液不易随烟气逃逸造成损失及二次污染；通过洗涤分段和除沫分段对烟气的两次洗涤和一次除沫，对烟气可能挟带的溶液成分形成三重拦截，使溶液成分较难随烟气逃逸，在一些较理想的情况下，烟气洗涤段01机会可以拦截烟气中挟带的全部溶液成分。
可选地，本申请实施例所提供的二氧化碳捕集塔，还包括洗涤液循环系统，所述洗涤分段和所述除沫分段均与所述洗涤液循环系统连接，所述洗涤液循环系统用于向所述洗涤分段和所述除沫分段供给洗涤液，且所述洗涤液循环系统用于接收从所述洗涤分段和所述除沫分段流出的洗涤液。这样，通过洗涤液循环系统可以对洗涤液进行循环再利用，节省成本；优选的，使洗涤液循环系统具有补水功能，当出现洗涤液损失时，可以补充作为洗涤液的除盐水。
优选的，本申请实施例中所为各填料均提供了用于支撑和固定填料的附属组件，附属组件可包括支撑梁11、支撑格栅14和压板15等，例如，本申请实施例中，预洗除杂段04还包括支撑梁11、支撑格栅14和压板15，并使气体分布器13、第一集液器12、支撑梁11、支撑格栅14、除杂填料10、压板15、预洗液分布器03和预洗液进料管16从下到上依次排列，支撑梁11和支撑格栅14用于支撑除杂填料10，压板15则用来压紧除杂填料10。本申请实施例中，烟气洗涤段01和预洗除杂段04所采用的填料优选为PP(中文名称为聚丙烯)材料，二氧化碳吸收段02所采用的填料优选为304不锈钢材质，如304不锈钢规整波纹填料、304不锈钢规整填料或304金属蜂窝斜板填料等。本申请实施例中预洗液优选为低浓度氢氧化钠水溶液，即碱液。
为了更好的说明本申请所提供的二氧化碳捕集塔，本申请还提供一种二氧化碳捕集塔的应用实例，在该应用实例中，预洗除杂段04还称为预洗段，二氧化碳吸收段02还称为吸收段，烟气洗涤段01还称为洗涤段，支撑梁11还称为填料支撑梁，二氧化碳捕集塔还称为复合吸收塔。该应用实例具体如下：
本应用实例涉及一种用于二氧化碳捕集的新型复合吸收塔，兼具传统工艺中的预洗塔和吸收塔的功能，即烟气在CO2复合吸收塔内经过洗涤、降温、回收CO2，再洗涤、降温后从CO2复合吸收塔顶部排放。
烟气CO2捕集的基本工艺流程主要由三部分组成：以吸收塔为中心，辅以预洗、气水分离及增压设备；以再生塔和再沸器为中心，辅以再生气、冷却气以及分离器和回流系统；介于以上两者之间的部分，主要有富CO2吸收液、再生吸收液换热系统以及过滤系统。
出口排放的烟气温度约为48℃，为胺溶液理想吸收温度区间。在预洗塔中对烟气进行预处理，除去烟气携带的微量石膏等杂质。使用增压风机克服气体通过预处理系统和吸收塔时的阻力。
在吸收塔中，烟气自下向上流动，与从上部喷淋入塔的胺溶液逆流接触，使CO2得到脱除，尾气由塔顶排入大气。为了防止溶液随烟气的逃逸造成损失及二次污染，吸收塔顶部设置尾气洗涤段，通过直接喷淋水洗，回收烟气携带的溶液成分。洗涤水循环利用，当捕集系统需要补水时，首先将洗涤水作系统补水，损失的洗涤水由除盐水补充。
吸收CO2后的富液由塔底经泵送入贫富液换热器，喷淋进入再生塔上部，通过汽提解吸部分CO2。经汽提解吸后的半贫液进入再沸器，使其中CO2进一步解吸。经再沸器解吸CO2后的贫液由再生塔底流出，经贫富液换热器、贫液冷却器冷却后，进入吸收塔循环使用。溶剂往返循环构成连续吸收和解吸CO2的工艺过程。
解吸出的CO2连同水蒸气经冷却后，分离除去水分后得到高纯度的CO2气，送入之后的压缩系统。再生气中被冷凝分离出来的冷凝水，用泵送至再生塔，对再生塔内温度进行调节。
为了维持溶液清洁，约10-15％的贫液经过活性炭过滤器过滤；为处理系统的降解产物，设置溶液净化回收系统，需要时，将部分贫液送入净化回收系统，加入定配的碱液进行净化回收。
在上述工艺中，预洗塔和吸收塔分开设置，存在以下问题：1)双塔及其相对完整的辅助系统配置致使系统流程相对复杂，控制要求高，项目初投资高，后期运行检修维护工作量大；2)由于设置两个塔，占地面积较单塔大，应用受场地制约明显；3)对负荷适应性较差，低负荷工况下能耗较高。
本应用实例提出的复合吸收塔，将预洗塔和吸收塔合二为一，来自机组脱硫系统后的烟气首先进入复合吸收塔的预洗段，对烟气进行预处理，除去烟气携带的微量石膏等杂质；然后再进入复合吸收塔的吸收段，进行脱碳处理；最后烟气再进入洗涤段，回收烟气携带的溶液成分。即烟气在CO2复合吸收塔内经过洗涤、降温、回收CO2，再洗涤、降温后从CO2复合吸收塔顶部进行排放。
与双塔(预洗塔和吸收塔)相比，复合吸收塔的优点：1)双塔合一，碳捕集系统流程相对简单，项目初投资较低，后期运行的检修维护工作量较小；2)占地面积较单塔小，应用受场地制约程度小；3)操作方便，对负荷适应性较高，低负荷工况下能耗较低。
复合吸收塔从下至上包括预洗段、吸收段和洗涤段，烟气从塔底部进入复合吸收塔，其中，各个部分的作用如下：
(1)在预洗段，对烟气进行预处理，除去烟气携带的微量石膏等杂质。
(2)在吸收段，烟气自下向上流动，与从上部喷淋入塔的碳捕集吸收溶液逆流接触，使CO2得到脱除，尾气进入洗涤段。
(3)在预洗段和吸收段设置带有雾沫捕集装置的液体收集器，防止捕集溶液漏液到预洗段。
(4)在洗涤段，通过直接喷淋水洗，回收烟气携带的溶液成分，避免溶液随烟气的逃逸造成损失及二次污染。洗涤水可循环利用，当捕集系统需要补水时，首先将洗涤水作系统补水，损失的洗涤水由除盐水补充。
复合吸收塔的详细方案，各段具体结构如下：
(1)预洗段(Bed6)，结构布置从下到上依次应是气体分布器、集液器、填料支撑梁、支撑格栅、填料、压板、液体分布器、进料管；
(2)吸收段(Bed3-5)，Bed5的结构布置从下到上依次应是集液器、填料及其附属组件；Bed4的结构布置依次应是集液器、填料及其附属组件、液体分布器、中间吸收冷却进料管；Bed3的结构布置依次应是集液器、填料及其附属组件、液体分布器、贫液进料管；
(3)尾气洗涤段(Bed1-2)，Bed2的结构布置依次应是集液器、填料及其附属组件、液体分布器、下段洗涤液进料管；Bed1的结构布置依次应是集液器、填料及其附属组件、液体分布器、上段洗涤液进料管、丝网除沫器及其附属组件。
本应用实例提出的复合吸收塔，将预洗塔和吸收塔合二为一，来自机组脱硫系统后的烟气首先进入复合吸收塔的预洗段，对烟气进行预处理，除去烟气携带的微量石膏等杂质；然后再进入吸收塔，进行脱碳处理；最后烟气再进入洗涤段，回收烟气携带的溶液成分。即烟气在CO2复合吸收塔内经过洗涤，降温、回收CO2，再洗涤、降温后从CO2复合吸收塔顶部进行排放。
与双塔(预洗塔和吸收塔)相比，复合吸收塔的优点：1)双塔合一，碳捕集系统流程相对简单，项目初投资较低，后期运行的检修维护工作量较小；2)占地面积较单塔小，应用受场地制约程度小；3)操作方便，对负荷适应性较高，低负荷工况下能耗较低。
最后应说明的是：以上各实施例仅用以说明本申请的技术方案，而非对其限制；尽管参照前述各实施例对本申请进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本申请各实施例技术方案的范围。

Claims (10)

1.二氧化碳捕集塔，其特征在于，包括在竖直方向上从下到上依次排列的预洗除杂段、二氧化碳吸收段和烟气洗涤段，以使烟气能够依次流经预洗除杂段、二氧化碳吸收段和烟气洗涤段，在所述预洗除杂段上设置有二氧化碳捕集塔烟气入口，在所述洗涤段上设置有二氧化碳捕集塔烟气出口。
根据权利要求1所述的二氧化碳捕集塔，其特征在于，所述预洗除杂段包括从下到上依次排列的气体分布器、第一集液器、除杂填料、预洗液分布器和预洗液进料管，所述预洗液进料管与所述预洗液分布器连通以通过所述预洗液进料管向所述预洗液分布器供给用于预洗烟气的预洗液。
根据权利要求1所述的二氧化碳捕集塔，其特征在于，所述二氧化碳吸收段包括在竖直方向上排列的多个分段，各所述分段之一为集液分段，在各所述分段中所述集液分段位于最下方，所述集液分段包括液体收集器，所述液体收集器包括雾沫捕集件。
根据权利要求3所述的二氧化碳捕集塔，其特征在于，各所述分段之一为贫液吸收分段，所述贫液吸收分段包括从下到上依次排列的第二集液器、第一吸收填料、贫液分布器和贫液进料管，所述第二集液器用于供烟气通过，所述贫液进料管与所述贫液分布器连通。
根据权利要求4所述的二氧化碳捕集塔，其特征在于，各所述分段之一为冷却吸收分段，所述集液分段、所述冷却吸收分段和所述贫液吸收分段从下到上依次排列，所述冷却吸收分段用于冷却烟气并吸收烟气中的二氧化碳。
根据权利要求5所述的二氧化碳捕集塔，其特征在于，所述冷却吸收分段包括从下到上依次排列的第三集液器、第二吸收填料、吸收冷却液分布器和吸收冷却液进料管，所述第三集液器用于供烟气通过，所述吸收冷却液进料管与所述吸收冷却液分布器连通。
根据权利要求1-6中任意一项所述的二氧化碳捕集塔，其特征在于，所述烟气洗涤段包括洗涤分段和除沫分段，所述洗涤分段位于所述除沫分段的下方。
根据权利要求7所述的二氧化碳捕集塔，其特征在于，所述除沫分段包括从下到上依次排列的第四集液器、第一洗涤填料、第一洗涤液分布器、第一洗涤液进料管和丝网除沫器，所述第一洗涤液进料管与所述第一洗涤液分布器连通，所述第四集液器用于供烟气通过。
根据权利要求7所述的二氧化碳捕集塔，其特征在于，所述洗涤分段包括第五集液器、第二洗涤填料、第二洗涤液分布器和第二洗涤液进料管，所述第二洗涤液分布器与第二洗涤液进料管连通，所述第五集液器用于供烟气通过。
根据权利要求7所述的二氧化碳捕集塔，其特征在于，还包括洗涤液循环系统，所述洗涤分段和所述除沫分段均与所述洗涤液循环系统连接，所述洗涤液循环系统用于向所述洗涤分段和所述除沫分段供给洗涤液，且所述洗涤液循环系统用于接收从所述洗涤分段和所述除沫分段流出的洗涤液。
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