WO2025256083A1 - 二氧化碳捕集系统和方法及应用 - Google Patents

二氧化碳捕集系统和方法及应用

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Publication number
WO2025256083A1
WO2025256083A1 PCT/CN2024/138466 CN2024138466W WO2025256083A1 WO 2025256083 A1 WO2025256083 A1 WO 2025256083A1 CN 2024138466 W CN2024138466 W CN 2024138466W WO 2025256083 A1 WO2025256083 A1 WO 2025256083A1
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WIPO (PCT)
Prior art keywords
carbon dioxide
liquid
unit
desorption
flue gas
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/CN2024/138466
Other languages
English (en)
French (fr)
Inventor
蔡勇
高飞
魏弢
刘克峰
刘陶然
董卫刚
周华群
胡雪生
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.)
Petrochina Co Ltd
Original Assignee
Petrochina Co Ltd
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Filing date
Publication date
Application filed by Petrochina Co Ltd filed Critical Petrochina Co Ltd
Publication of WO2025256083A1 publication Critical patent/WO2025256083A1/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
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/02—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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 invention relates to the field of carbon dioxide capture technology, and more specifically to a carbon dioxide capture system, method, and application.
  • Carbon dioxide capture technology has become one of the key research areas globally to address global warming and reduce carbon dioxide emissions into the atmosphere. Future research needs to tackle the challenges and difficulties of these technologies and methods to overcome current bottlenecks and promote the economic viability, efficiency, and scalability of carbon dioxide capture technology.
  • Carbon dioxide capture (CO2) technology is a key carbon reduction technology that can effectively reduce CO2 emissions and slow the rate of global warming.
  • CO2 capture technologies broadly include pre-combustion capture, post-combustion capture, oxy-fuel combustion, and chemical looping combustion.
  • Each technology has its advantages and limitations; currently, no single technology can independently meet the requirements of high efficiency, low cost, low energy consumption, and large-scale operation.
  • Post-combustion capture involves capturing CO2 after fuel combustion. This method has the advantage of capturing CO2 produced during combustion, but it may require higher energy consumption and costs.
  • Common technologies include amine absorption and carbonate absorption.
  • CN201510529951.2 discloses a carbon dioxide capture system, including an absorption tower having: a first inlet connected to a fan outlet; a first outlet located at the top of the absorption tower; a second inlet located at the upper part of the absorption tower; and a second outlet located at the bottom of the absorption tower.
  • This technology uses traditional absorption towers, and the maintenance and repair costs of carbon steel + anti-corrosion layer and alloy absorption towers are increasing year by year.
  • CN201910171708.6 discloses a circulating pretreatment system for carbon dioxide capture in coal-fired power plants, including a water washing tower, multiple packing layers arranged from bottom to top inside the water washing tower, a circulating water cooler, an automatic alkali addition device, and a salinity adjustment device.
  • This pretreatment system employs a combination of multiple packing layers to thoroughly remove harmful substances such as dust and SO2 from the flue gas, improving washing efficiency and reducing flue gas temperature.
  • the external washing tower is equipped with an automatic alkali addition device and a salinity adjustment device, which automatically adjusts the alkali dosage based on the pH setting of the circulating washing water to effectively remove acidic substances from the flue gas, ensuring the washing effect.
  • Flue gas commonly contains nitrogen oxides, sulfur oxides, and dust, and generally requires pretreatment before entering the absorption tower.
  • the water washing tower used in this technology suffers from low transfer efficiency and poor mass transfer.
  • the purpose of this invention is to overcome the problems of high capture cost and difficulty in scaling up large-scale carbon capture and absorption towers in the existing technology, and to provide a carbon dioxide capture system, method and application with the advantages of low cost and low energy consumption.
  • a first aspect of the present invention provides a carbon dioxide capture system, the carbon dioxide capture system comprising:
  • a pretreatment unit for removing dust from flue gas containing carbon dioxide including a cyclone separator having a liquid phase feeder that distributes the washing liquid in a mist and a cyclone structure that forms a cyclone in the flue gas to contact the washing liquid.
  • the absorption unit is connected to the gas phase outlet of the pretreatment unit and is used to bring the carbon dioxide absorbent into contact with the flue gas to form a rich liquid.
  • the desorption unit is connected to the rich liquid outlet of the absorption unit and is used to desorb carbon dioxide from the rich liquid under hypergravity to obtain a lean liquid.
  • a heat exchange unit is used to collect the heat discharged from the desorption unit.
  • This invention provides a carbon dioxide capture method, performed in the system of this invention, the method comprising the following steps:
  • the flue gas containing carbon dioxide is formed into a swirling flow, so that the washing liquid is dispersed and comes into contact with the swirling flue gas to remove dust from the flue gas.
  • step 2) The flue gas treated in step 1) is contacted with a carbon dioxide absorbent to form a rich liquid;
  • step 3) The heat collected from the discharge in step 3) is used to achieve heat recovery and reuse of the discharged material.
  • This invention provides the application of the carbon dioxide capture method and/or carbon dioxide capture system of this invention in the capture of carbon dioxide of more than 500,000 tons/year.
  • the carbon dioxide capture system of the present invention adopts supergravity coupled heat collection technology to realize the comprehensive utilization of heat. Compared with traditional desorption technology, the desorption energy consumption can be reduced by more than 15-20%, and the carbon dioxide capture cost can be significantly reduced in large-scale carbon capture.
  • the carbon dioxide capture method of this invention uses supergravity desorption to break the rich liquid into droplets, liquid lines and liquid films, thereby improving the efficiency of heat and mass utilization. Combined with heat collection technology, it can realize the comprehensive utilization of heat and reduce energy consumption. Furthermore, the use of concrete absorption towers can extend service life and reduce maintenance frequency. In large-scale carbon capture, the cost of carbon dioxide capture can be significantly reduced, and it has the advantages of high efficiency, low cost, low energy consumption and large scale.
  • Figure 1 is a schematic flowchart of a carbon dioxide capture system according to some embodiments of the present invention.
  • Figure 2 is a schematic diagram of the structure of a cyclone separator according to some embodiments of the present invention.
  • Figure 3 is a schematic diagram of the structure of a concrete absorption tower according to some embodiments of the present invention.
  • Figure 4 is a schematic diagram of the structure of the supergravity desorption device according to some embodiments of the present invention.
  • Figure 5 is a structural schematic diagram of the supergravity desorption device according to some other embodiments of the present invention.
  • Figure 6 is a structural schematic diagram of a mobile bed according to some embodiments of the present invention.
  • Pretreatment unit 1-1 Tangential flue gas inlet; 1-2 Liquid phase feed unit; 1-3 Gas phase outlet; 1-4 Liquid phase outlets; 2 Absorption units; 2-1 Flue gas inlet; 2-2 Carbon dioxide absorbent/lean liquor inlet; 2-3 Exhaust gas outlet; 2-4 Rich liquid outlet; 2-5 Packing unit; 3 Desorption unit; 3-1-1 Housing; 3-1-2 Rotating shaft; 3-1-3 Bearing; 3-1-4 Microwave head; 3-1-5 Lateral lean liquid outlet; 3-1-6 Lateral gas inlet; 3-1-7 Rich liquid inlet; 3-1-8 Gas outlet; 3-2-1 Liquid inlet; 3-2-2 Air inlet; 3-2-3 Liquid outlet; 3-2-4 Gas outlet; 4. Lean liquor purification unit; 4-1. Mobile stand; 4-2 Purification tank; 5 Heat exchange unit.
  • directional terms such as “upper,” “lower,” “top,” and “bottom” are generally used to describe the relative positions of components in relation to the directions shown in the accompanying drawings or in relation to the vertical, perpendicular, or gravitational directions.
  • “Inner” and “outer” generally refer to the inner and outer parts of the cavity relative to the chamber or the radial inner and outer parts relative to the center of the circle.
  • This invention discloses a carbon dioxide capture system, as shown in Figure 1, which includes:
  • Pretreatment unit 1 is used to remove dust from flue gas containing carbon dioxide.
  • the pretreatment unit 1 includes a cyclone separator.
  • the cyclone separator has a liquid phase feeder 1-2 that makes the washing liquid a mist distribution and a cyclone structure that makes the flue gas form a cyclone and contact the washing liquid.
  • Absorption unit 2 is connected to the gas phase outlet of pretreatment unit 1 and is used to bring carbon dioxide absorbent into contact with flue gas to form a rich liquid.
  • Desorption unit 3 is connected to the rich liquid outlet of absorption unit 2 and is used to desorb carbon dioxide from the rich liquid under hypergravity to obtain a lean liquid.
  • Heat exchange unit 5 is used to collect the heat discharged from desorption unit 3.
  • the carbon dioxide capture system of this invention adopts supergravity coupled heat collection technology to achieve comprehensive utilization of heat. Compared with traditional desorption technology, the desorption energy consumption can be reduced by more than 15-20%, and the carbon dioxide capture cost can be significantly reduced in large-scale carbon capture.
  • the pretreatment unit 1 includes a hydrocyclone separator, as shown in Figure 2.
  • a washing liquid feed pipe is provided at the top of the hydrocyclone separator.
  • the discharge end of the washing liquid feed pipe is provided with a liquid phase feed element 1-2 that disperses the liquid phase.
  • the hydrocyclone separator is provided with a cyclone structure that allows the flue gas to form a cyclone and contact the washing liquid.
  • the swirling structure there are no special requirements for the swirling structure, as long as the flue gas can form a swirling flow and come into contact with the washing liquid.
  • the swirling separator is provided with a cavity with a circular cross-section, and the swirling structure can be set as a tangential flue gas inlet 1-1 opened in the cavity, so that the flue gas forms a swirling flow by tangentially feeding into the cavity.
  • the liquid phase feeders 1-2 there are no special requirements for the liquid phase feeders 1-2, as long as they can disperse the washing liquid as much as possible.
  • the liquid phase feeders can adopt the high-speed rotating titanium metal disk structure in the prior art.
  • the hydrocyclone separator can be installed in the pretreatment tower.
  • the gas phase outlet 1-4 of the hydrocyclone separator is connected to the top of the pretreatment tower, and the liquid phase outlet 1-3 of the hydrocyclone separator can be connected to the liquid phase feed 1-2 through the water washing liquid circulation pipeline to realize the recycling of the water washing liquid.
  • the absorption unit 2 includes a concrete absorption tower, as shown in Figure 1.
  • the concrete absorption tower has, from top to bottom, a tail gas outlet 2-3, a carbon dioxide absorbent/lean liquor inlet 2-2, a flue gas inlet 2-1, and a rich liquor outlet 2-4.
  • the flue gas inlet 2-1 connects to the top of the pretreatment tower, allowing the flue gas from the pretreatment unit 1 to come into countercurrent contact with the carbon dioxide absorbent.
  • the carbon dioxide absorbent can be fresh or lean liquor, as shown in Figure 3.
  • a wire mesh demister is installed between the tail gas outlet 2-3 and the carbon dioxide absorbent/lean liquor inlet 2-2.
  • Each packing unit 2-5 has an absorbent distributor, a packing layer, and a liquid collector arranged sequentially from top to bottom.
  • the packing layer uses regular packing.
  • the feed end of the absorbent distributor in the first packing unit is connected to the carbon dioxide absorbent/lean liquid feed inlet 2-2.
  • the liquid collector of the previous unit is connected to the feed end of the absorbent distributor of the next unit.
  • the nozzle of the absorbent distributor in each packing unit is an atomizing nozzle in the prior art. It can be understood that the higher the atomization degree of the atomizing nozzle, the better the initial dispersion efficiency of the carbon dioxide absorbent and/or lean liquid.
  • desorption refers to the decomposition reaction of unstable salts formed by amine molecules and CO2 upon heating ( ⁇ 100°C), resulting in CO2 diffusion from the liquid phase to the gas phase, achieving CO2 separation and solvent regeneration.
  • the thermal decomposition reaction is the reverse of the absorption process.
  • the reaction kinetics are instantaneous and rapid. Therefore, the instantaneous nature of the desorption reaction kinetics determines that the rate of CO2 molecule mass transfer from the liquid phase to the gas phase is the rate-controlling step of the entire desorption reaction-mass transfer coupling process.
  • the supergravity technology in this invention can enhance the mass transfer effect for this type of process, effectively improving the weaknesses of traditional tower equipment, such as low gas-liquid mass transfer efficiency and large reactor volume.
  • the desorption unit 3 includes a hypergravity desorption device, as shown in FIG4.
  • the hypergravity desorption device includes a housing 3-1-1 surrounding a defined desorption chamber.
  • An axially extending rotating shaft 3-1-2 is provided in the desorption chamber.
  • the rotating shaft 3-1-2 is connected to the housing 3-1-1 via a bearing 3-1-3.
  • Microwave heads 3-1-4 are arranged axially at intervals on the rotating shaft 3-1-2.
  • the top of the housing 3-1-1 has a rich liquid inlet 3-1-7, the upper part has a lateral gas inlet 3-1-6, the lower part has a lateral lean liquid outlet 3-1-5, and the bottom has a gas outlet 3-1-8.
  • a motor is installed at the top of the housing 3-1-1.
  • the motor is connected to the rotating shaft via an electric slip ring.
  • a cable groove is provided on the rotating shaft for installing cables.
  • the microwave heads are electrically connected to the electric slip ring via cables.
  • the fixed outer ring of the slip ring is connected to an external power source, and the sliding inner ring is tightly clamped to the rotating shaft 3-1-2.
  • the power source of the inner ring is fixed to the rotating shaft 3-1-2 through a wire groove to power the microwave probe.
  • the rich liquid enters from the side rich liquid inlet, and the hot hydrogen enters from the side gas inlet 3-1-6, making the rotating shaft rotate at 400-1500 rpm.
  • the rich liquid is desorbed, and the resulting lean liquid is discharged from the side lean liquid outlet 3-1-5.
  • the desorbed CO2 is discharged from the gas outlet 3-1-8.
  • the coupling of microwave and rotating shaft can reduce desorption temperature and desorption energy consumption.
  • Thermal desorption of amine-rich liquid is achieved in the presence of microwave, while accelerating the flow of amine-rich liquid and improving heat and mass transfer efficiency.
  • it can reduce desorption energy consumption, shorten the process flow, eliminate the need for a reboiler, and reduce process connections with process engineering steam.
  • the supergravity desorption device of the desorption unit 3 is not limited to that shown in FIG4, but can also adopt the centrifugal dispersion device disclosed in CN 116328496 A, as shown in FIG5.
  • the top of the shell of the centrifugal dispersion device is provided with a liquid inlet 3-2-1 and an air outlet 3-2-4, the bottom of the shell is provided with a liquid outlet 3-2-3, and the side of the shell is provided with an air inlet 3-2-2.
  • the air inlet 3-2-2 is connected to the hydrogen feed line.
  • the liquid outlet 3-2-3 of the centrifugal dispersion device When steam is used to desorb the rich liquid, the liquid outlet 3-2-3 of the centrifugal dispersion device is connected to the air inlet 3-2-2, and a reboiler is provided on the connecting pipeline. In this way, the lean liquid is discharged from the liquid outlet 3-2-3 and fed into the reboiler to generate steam, which enters through the air inlet 3-2-2.
  • the heat exchange unit can use a heat pump component in the prior art (such as a York YHAP-C lithium bromide heat pump component) to collect and heat up the material discharged from the gas outlet 3-1-8 or the gas outlet 3-2-4 of the desorption unit 3 to provide heat for the desorption of the desorption unit 3.
  • a heat pump component such as a York YHAP-C lithium bromide heat pump component
  • the present invention can break the rich liquid into droplets, liquid lines and liquid films through the supergravity technology, improve the heat and mass utilization efficiency, and further reduce the energy consumption in the desorption process by combining the heat pump component.
  • large-scale carbon capture greater than 500,000 tons/year, it has the advantage of lower engineering cost.
  • the lean liquid outlet or outlet 3-2-3 of the desorption unit 3 is connected to the absorption unit 2 through a lean liquid pipeline, so that the lean liquid obtained after desorption is returned to the absorption unit to contact the flue gas and absorb carbon dioxide.
  • a lean solution purification unit 4 is preferably installed on the lean solution pipeline to remove thermally stable salts from the lean solution.
  • the lean solution purification unit 4 includes a moving bed, which includes at least one bed layer.
  • Each bed layer includes a moving frame 4-1 capable of moving around the center of the moving bed, and a plurality of purification tanks 4-2 are installed at intervals along the length of the moving frame.
  • the moving frame can be configured to be circular and rotatable, and six purification tanks 4-2 are installed at intervals along the circumference of the moving frame, so that the lean solution enters each purification tank sequentially to remove the thermally stable salts in the lean solution.
  • the moving bed can be configured with two bed layers stacked along the height direction, and the two bed layers can be alternately used to achieve lean solution purification.
  • this invention discloses a carbon dioxide capture method, which is performed in the system of this invention and includes the following steps:
  • the flue gas containing carbon dioxide is formed into a swirling flow, so that the washing liquid is dispersed and comes into contact with the swirling flue gas to remove dust from the flue gas.
  • step 2) The flue gas treated in step 1) is contacted with a carbon dioxide absorbent to form a rich liquid;
  • the carbon dioxide capture method of the present invention adopts supergravity coupled heat collection technology to realize the comprehensive utilization of heat. Compared with traditional desorption technology, the desorption energy consumption can be reduced by more than 15-20%, and the carbon dioxide capture cost can be significantly reduced in large-scale carbon capture.
  • step 1) the flue gas is made into a swirling flow, allowing the washing liquid to disperse and contact with the swirling flue gas.
  • flue gas from industrial plants including refinery catalytic cracking units, refinery ammonia synthesis units, refinery hydrogen production units, and coal-fired boilers in power plants, generally contains nitrogen oxides, sulfur oxides, dust, and other substances.
  • the existing water washing tower method has the defects of low transfer efficiency and poor mass transfer, especially in large-scale carbon capture, where these defects will be amplified.
  • This invention makes the flue gas into a swirling flow, breaking the washing liquid into liquid films, liquid lines, and droplets, increasing the specific surface area for mass transfer, reducing the amount of washing liquid used, and improving the treatment effect.
  • the washing solution in this invention has no special requirements.
  • it can be an alkaline solution that can remove sulfur oxides or water.
  • the alkaline solution can be a commonly used sodium hydroxide aqueous solution.
  • the range of conditions for contact between flue gas and carbon dioxide absorbent is relatively wide.
  • the following is an illustrative description, but it does not limit the scope of this invention.
  • the conditions for contact between flue gas and carbon dioxide absorbent in step 2) include: temperature range of 40-50°C and normal pressure.
  • the carbon dioxide absorbent is selected from at least one of MDEA, MEA, AEEA, and PZ.
  • the flue gas and carbon dioxide absorbent in step 2) are contacted in a concrete absorption tower.
  • concrete absorption towers have a lower maintenance and repair probability over a service life of several decades. They have advantages such as fire resistance, durability, low overall cost, and strong design flexibility, resulting in better overall benefits.
  • concrete absorption towers can accommodate more large internal components. More importantly, with the trend of towers becoming larger, concrete absorption towers that are tens or even hundreds of meters high are increasingly showing advantages in saving initial investment. Taking large-scale low-concentration carbon dioxide capture as an example, compared with the existing metal absorption towers, concrete absorption towers can significantly reduce carbon dioxide capture costs. Moreover, concrete towers can be cast in one piece on site using molds, overcoming the construction difficulties of large towers; at the same time, based on anti-corrosion technology, long-term operation of large-scale carbon capture can be achieved.
  • the inner wall of the concrete absorption tower is treated with existing technology to form an anti-corrosion layer.
  • corrosion-resistant bricks and anti-corrosion adhesives can be used to integrate the wall anti-corrosion and the tower structure through a composite inlay process.
  • the desorption of amine-rich liquid is mainly achieved by feeding it into the top of the regeneration tower, where it comes into contact with the hot steam flowing counter-currently from the bottom.
  • the contact state between the gas and liquid cannot be easily controlled inside the regeneration tower, and there is often a defect of insufficient heat transfer. Therefore, this invention adopts centrifugal desorption, which uses centrifugal force to break up the amine-rich liquid and improve the efficiency of heat and mass utilization.
  • the amine-rich liquid is desorbed under microwave and centrifugal conditions. This invention uses a combination of microwave and centrifugal methods to achieve good desorption effect while reducing desorption energy consumption.
  • the volume content of carbon dioxide in the flue gas containing carbon dioxide is 10-30%.
  • the microwave frequency is 2450 ⁇ 50 MHz.
  • the hypergravity operating conditions include a rotational speed of 400-1200 rpm.
  • hot hydrogen and/or steam can be used to desorb the rich liquid.
  • hot hydrogen is preferably used to desorb the rich liquid.
  • the hydrogen and carbon dioxide obtained after desorption can be further used to prepare methanol or low-carbon olefins. More preferably, the temperature of the hot hydrogen is 90-108°C.
  • the volumetric flow rate ratio of hot hydrogen to rich liquid is 30-60:1.
  • the lean liquid from step 3) is returned to step 2) to contact the flue gas from step 1) to absorb carbon dioxide.
  • the lean liquid from step 3) is purified and then returned to step 2) to contact the flue gas from step 1) to absorb carbon dioxide.
  • ion exchange resin is used to continuously purify lean liquor.
  • the range of selectable purification conditions is relatively wide.
  • the purification conditions include: normal temperature and normal pressure.
  • step 4 a heat pump is used to collect the heat from the output in step 3).
  • This invention discloses the application of the carbon dioxide capture method and/or the carbon dioxide capture system of this invention in the capture of carbon dioxide exceeding 500,000 tons/year.
  • a carbon dioxide detector is used for evaluation and analysis.
  • the capture efficiency is calculated as the ratio of the carbon dioxide concentration at the outlet of the concrete absorption tower to the carbon dioxide concentration at the inlet.
  • the carbon dioxide purity is calculated as the ratio of the carbon dioxide content in the desorbed gas to the total content of the desorbed gas.
  • the concrete in the concrete absorption tower has a strength of C40 and a seismic resistance level of 7.
  • This embodiment uses the carbon dioxide capture system shown in Figure 1, which includes: a pretreatment unit 1, an absorption unit 2, a desorption unit 3, a lean solution purification unit 4, and a heat exchange unit 5.
  • the pretreatment unit 1 includes a cyclone separator, with a washing liquid feed pipe at the top of the cyclone separator.
  • the discharge end of the washing liquid feed pipe is equipped with a high-speed rotating titanium metal disc structure.
  • the cross-section of the cyclone separator is a circular cavity, and the cyclone structure is set as a tangential flue gas inlet 1-1 opened in the cavity.
  • the absorption unit 2 includes a concrete absorption tower.
  • the concrete absorption tower has, from top to bottom, a tail gas outlet 2-3, a carbon dioxide absorbent/lean liquor inlet 2-2, a flue gas inlet 2-1, and a rich liquor outlet 2-4.
  • the flue gas inlet 2-1 is connected to the top of the pretreatment tower.
  • a wire mesh demister is installed between the tail gas outlet 2-3 and the carbon dioxide absorbent/lean liquor inlet 2-2.
  • Multiple packing units 2-5 are spaced apart along the height between the carbon dioxide absorbent/lean liquor inlet 2-2 and the flue gas inlet 2-1.
  • Each packing unit 2-5 has, from top to bottom, an absorbent distributor, a packing layer, and a liquid collector.
  • the feed end of the absorbent distributor in the first packing unit is connected to the carbon dioxide absorbent/lean liquor inlet 2-2.
  • the liquid collector of the previous unit is connected to the feed end of the absorbent distributor of the next unit.
  • the desorption unit 3 adopts the centrifugal dispersion device shown in Figure 5.
  • the top of the shell of the centrifugal dispersion device is provided with a liquid inlet 3-2-1 and an air outlet 3-2-4.
  • the bottom of the shell is provided with a liquid outlet 3-2-3 and the side of the shell is provided with an air inlet 3-2-2.
  • the liquid outlet 3-2-3 of the centrifugal dispersion device is connected to the air inlet 3-2-2 and a reboiler is provided on the connecting pipeline.
  • the lean liquid purification unit 4 includes a moving bed, which includes two bed layers. Each bed layer includes a circular moving frame 4-1 that can move around the center of the moving bed. Six purification tanks 4-2 are installed at intervals along the circumference of the moving frame. The outlet 3-2-3 of the desorption unit 3 is connected to the carbon dioxide absorbent/lean liquid inlet 2-2 through a lean liquid pipeline, which is connected to the purification tanks 4-2.
  • the heat exchange unit 5 includes a York YHAP-C lithium bromide heat pump assembly.
  • the heat input line of the York YHAP-C lithium bromide heat pump assembly is connected to the gas outlet 3-2-4, and the two ends of the heat output line are connected to the liquid outlet 3-2-3 and the liquid inlet 3-2-1, respectively.
  • the aforementioned carbon dioxide capture system treats flue gas from a power plant (carbon dioxide volume content 13.5%).
  • the gas is introduced through tangential flue gas inlet 1-1 to form a swirling flow, where it comes into contact with a washing liquid fed through a high-speed rotating titanium metal disc structure.
  • the pretreated flue gas is cooled to 45°C and dust particles are removed by water washing. Contact conditions include a temperature of 45°C and atmospheric pressure.
  • the pretreated flue gas enters the flue gas inlet 2-1 of the concrete absorption tower.
  • a mixed amine aqueous solution (mass concentration of 35% based on amine) enters the concrete absorption tower through the carbon dioxide absorbent/lean liquid inlet 2-2.
  • the amine solution reacts countercurrently with carbon dioxide, achieving a capture efficiency of 98%, forming a rich amine solution which exits through the rich liquid outlet 2-3.
  • -4 enters the supergravity desorption unit 3.
  • the desorption unit 3 uses a centrifugal dispersion device as shown in Figure 5 to contact the steam (temperature 105°C) from the reboiler in countercurrent.
  • the centrifugal dispersion device rotates at 450 r/min, and the steam to rich amine liquid feed volume flow ratio is 50:1.
  • the rich amine liquid undergoes a desorption reaction (desorption pressure is atmospheric pressure) and becomes lean amine liquid.
  • the lean amine liquid passes through a moving bed on the lean liquid pipeline and is desorbed by ion exchange resin under normal temperature and pressure conditions to remove thermally stable salts. Then it returns to the concrete tower through the carbon dioxide absorbent/lean liquid inlet 2-2.
  • the desorbed carbon dioxide and lean amine liquid exchange heat in the heat pump component.
  • the desorption energy consumption is 2.6 GJ/t CO2
  • the purity of the desorbed carbon dioxide reaches 97%.
  • the aforementioned carbon dioxide capture system is used to treat flue gas (30% carbon dioxide volume content) from the Daqing Petrochemical catalytic cracking unit.
  • the gas is introduced into the tangential flue gas inlet 1-1 to form a swirling flow, where it comes into contact with a washing liquid fed through a high-speed rotating titanium metal disc structure.
  • the pretreated flue gas is cooled to 45°C and dust particles are removed by water washing.
  • the contact conditions include a temperature of 45°C and atmospheric pressure. Subsequently, the pretreated flue gas enters the flue gas inlet 2-1 of the concrete absorption tower.
  • a mixed amine aqueous solution (35% by mass concentration of amine) enters the concrete absorption tower through the carbon dioxide absorbent/lean liquor inlet 2-2.
  • the amine solution reacts countercurrently with carbon dioxide, achieving a capture efficiency of 95%, forming a rich amine solution.
  • the liquid enters the high-gravity desorption unit 3 through the rich liquid outlet 2-4.
  • the desorption unit 3 uses a centrifugal dispersion device as shown in Figure 5 to contact the steam (temperature 105°C) from the reboiler in a countercurrent manner.
  • the centrifugal dispersion device rotates at 800 r/min, and the steam to rich amine liquid feed volume flow ratio is 35:1.
  • the rich amine liquid undergoes a desorption reaction (desorption pressure is atmospheric pressure) and becomes lean amine liquid.
  • the lean amine liquid passes through a moving bed on the lean liquid pipeline and is desorbed by ion exchange resin under ambient temperature and pressure conditions to remove thermally stable salts. Then it returns to the concrete tower through the carbon dioxide absorbent/lean liquid inlet 2-2.
  • the desorbed carbon dioxide and lean amine liquid exchange heat in the heat pump assembly.
  • the desorption energy consumption is 2.63 GJ/t CO2
  • the purity of the desorbed carbon dioxide reaches 96.5%.
  • the aforementioned carbon dioxide capture system is used to treat flue gas (18% carbon dioxide volume content) from the Daqing Petrochemical catalytic cracking unit.
  • the gas is introduced into the tangential flue gas inlet 1-1 to form a swirling flow, where it comes into contact with a water washing liquid fed through a high-speed rotating titanium metal disc structure.
  • the pretreated flue gas is cooled to 45°C and dust particles are removed by water washing.
  • the contact conditions include a temperature of 45°C and atmospheric pressure. Subsequently, the pretreated flue gas enters the flue gas inlet 2-1 of the concrete absorption tower.
  • a mixed amine aqueous solution (35% by mass concentration based on amine) enters the concrete absorption tower through the carbon dioxide absorbent/lean liquor inlet 2-2.
  • the amine solution reacts countercurrently with carbon dioxide, achieving a capture efficiency of 97%, forming a rich amine solution.
  • the solution enters the high-gravity desorption unit 3 through the rich solution outlet 2-4.
  • the desorption unit 3 uses a centrifugal dispersion device as shown in Figure 5 to contact the steam (temperature 105°C) from the reboiler in a countercurrent manner.
  • the centrifugal dispersion device rotates at 1150 r/min, and the steam to rich amine solution feed volume ratio is 60:1.
  • the rich amine solution undergoes a desorption reaction (desorption pressure is atmospheric pressure) and becomes lean amine solution.
  • the lean amine solution passes through a moving bed on the lean solution pipeline and is desorbed by ion exchange resin under ambient temperature and pressure conditions to remove thermally stable salts. Then, it returns to the concrete tower through the carbon dioxide absorbent/lean solution inlet 2-2.
  • the desorbed carbon dioxide and lean amine solution exchange heat in the heat pump assembly.
  • the desorption energy consumption can reach 2.57 GJ/t CO2 , and the purity of the desorbed carbon dioxide reaches 97.3%.
  • the desorption unit 3 adopts the hypergravity desorption device shown in Figure 4.
  • the hypergravity desorption device includes a housing 3-1-1 surrounding a defined desorption chamber.
  • An axially extending rotating shaft 3-1-2 is provided in the desorption chamber.
  • the rotating shaft 3-1-2 is connected to the housing 3-1-1 through a bearing 3-1-3.
  • Microwave heads 3-1-4 are arranged axially at intervals on the rotating shaft 3-1-2.
  • the top of the housing 3-1-1 has a rich liquid inlet 3-1-7, the upper part has a lateral gas inlet 3-1-6, the lower part has a lateral lean liquid outlet 3-1-5, and the bottom has a gas outlet 3-1-8.
  • a motor is installed at the top of the housing 3-1-1.
  • the motor is connected to the rotating shaft through an electric slip ring.
  • a cable groove is provided on the rotating shaft for installing cables.
  • the microwave heads are electrically connected to the electric slip ring through the cables.
  • the rich liquid inlet 3-1-7 of the supergravity desorption device is connected to the rich liquid outlet 2-4. Hot hydrogen is introduced into the side gas inlet 3-1-6 of the supergravity desorption device.
  • the lean liquid outlet 3-1-5 is connected to the carbon dioxide absorbent/lean liquid inlet 2-2 through a lean liquid pipeline.
  • the lean liquid pipeline is connected to the purification tank 4-2.
  • the heat exchange unit 5 includes a York YHAP-C lithium bromide heat pump assembly.
  • the heat input pipeline of the York YHAP-C lithium bromide heat pump assembly is connected to the gas outlet 3-1-8.
  • the two ends of the heat output pipeline are connected to the desorption chamber.
  • the rotating shaft 3-1-2 rotates at 800 rpm
  • the microwave head 3-1-4 has a frequency of 2450 MHz
  • the volume flow ratio of hot hydrogen gas (temperature 95°C) entering through the side gas inlet 3-1-6 to rich amine liquid entering through the rich liquid inlet 3-1-7 is 50:1.
  • the desorption unit 3 adopts the hypergravity desorption device shown in Figure 4.
  • the hypergravity desorption device includes a housing 3-1-1 surrounding a defined desorption chamber.
  • An axially extending rotating shaft 3-1-2 is provided in the desorption chamber.
  • the rotating shaft 3-1-2 is connected to the housing 3-1-1 through a bearing 3-1-3.
  • Microwave heads 3-1-4 are arranged axially at intervals on the rotating shaft 3-1-2.
  • the top of the housing 3-1-1 has a rich liquid inlet 3-1-7, the upper part has a lateral gas inlet 3-1-6, the lower part has a lateral lean liquid outlet 3-1-5, and the bottom has a gas outlet 3-1-8.
  • a motor is installed at the top of the housing 3-1-1.
  • the motor is connected to the rotating shaft through an electric slip ring.
  • a cable groove is provided on the rotating shaft for installing cables.
  • the microwave heads are electrically connected to the electric slip ring through the cables.
  • the rich liquid inlet 3-1-7 of the supergravity desorption device is connected to the rich liquid outlet 2-4. Hot hydrogen is introduced into the side gas inlet 3-1-6 of the supergravity desorption device.
  • the lean liquid outlet 3-1-5 is connected to the carbon dioxide absorbent/lean liquid inlet 2-2 through a lean liquid pipeline.
  • the lean liquid pipeline is connected to the purification tank 4-2.
  • the heat exchange unit 5 includes a York YHAP-C lithium bromide heat pump assembly.
  • the heat input pipeline of the York YHAP-C lithium bromide heat pump assembly is connected to the gas outlet 3-1-8.
  • the two ends of the heat output pipeline are connected to the desorption chamber.
  • the rotation speed of the shaft 3-1-2 is 800 rpm, and the volume flow ratio of the hot hydrogen gas (temperature 105°C) entering through the side gas inlet 3-1-6 to the rich amine liquid entering through the rich liquid inlet 3-1-7 is 50:1.
  • Example 1 for the carbon dioxide capture system treating flue gas (carbon dioxide volume content 12%) from the Daqing Petrochemical catalytic cracking unit, the desorption unit 3 does not have a reboiler.
  • the centrifugal dispersion equipment is connected to hot hydrogen from the process engineering pipeline network and comes into countercurrent contact with the rich amine liquid.
  • the feed volume flow ratio of hydrogen to rich amine liquid is 45:1.
  • the desorption unit 3 adopts the hypergravity desorption device shown in Figure 4.
  • the hypergravity desorption device includes a housing 3-1-1 surrounding a defined desorption chamber.
  • An axially extending rotating shaft 3-1-2 is provided in the desorption chamber.
  • the rotating shaft 3-1-2 is connected to the housing 3-1-1 through a bearing 3-1-3.
  • Microwave heads 3-1-4 are arranged axially at intervals on the rotating shaft 3-1-2.
  • the top of the housing 3-1-1 has a rich liquid inlet 3-1-7, the upper part has a lateral gas inlet 3-1-6, the lower part has a lateral lean liquid outlet 3-1-5, and the bottom has a gas outlet 3-1-8.
  • a motor is installed at the top of the housing 3-1-1.
  • the motor is connected to the rotating shaft through an electric slip ring.
  • a cable groove is provided on the rotating shaft for installing cables.
  • the microwave heads are electrically connected to the electric slip ring through the cables.
  • the rich liquid inlet 3-1-7 of the supergravity desorption device is connected to the rich liquid outlet 2-4. Steam is introduced into the lateral gas inlet 3-1-6 of the supergravity desorption device.
  • the lean liquid outlet 3-1-5 is connected to the carbon dioxide absorbent/lean liquid inlet 2-2 through a lean liquid pipeline.
  • the lean liquid pipeline is connected to the purification tank 4-2.
  • the heat exchange unit 5 includes a York YHAP-C lithium bromide heat pump assembly.
  • the heat input pipeline of the York YHAP-C lithium bromide heat pump assembly is connected to the gas outlet 3-1-8.
  • the two ends of the heat output pipeline are connected to the desorption chamber.
  • the rotating shaft 3-1-2 rotates at 800 rpm
  • the microwave head 3-1-4 has a frequency of 2450 MHz
  • the volume flow ratio of the steam (temperature 95°C) entering through the side gas inlet 3-1-6 to the rich amine liquid entering through the rich liquid inlet 3-1-7 is 50:1.
  • the desorption unit uses a regeneration tower with the same processing capacity as in the prior art for desorption.

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Abstract

本发明涉及二氧化碳捕集技术领域，公开了一种二氧化碳捕集系统和方法及应用，二氧化碳捕集系统包括预处理单元、吸收单元和热交换单元，预处理单元用于去除含有二氧化碳的烟气中的粉尘，预处理单元包括旋流分离器，旋流分离器具有使水洗液呈雾状分布的液相进料件和使烟气形成旋流与水洗液接触的旋流结构；吸收单元与预处理单元的气相出口相连通，用于使二氧化碳吸收剂与烟气接触形成富液；解吸单元与吸收单元的富液出口相连，用于使富液在超重力下进行解吸出二氧化碳并得到贫液；热交换单元用于收集解吸单元的出料热量。本发明具有低成本、低能耗的优势。

Description

二氧化碳捕集系统和方法及应用
相关申请的交叉引用
本申请要求2024年06月11日提交的中国专利申请202410747823.4的权益，该申请的内容通过引用被合并于本文。
技术领域
本发明涉及二氧化碳捕集技术领域，具体地涉及一种二氧化碳捕集系统和方法及应用。
背景技术
二氧化碳捕集技术已成为全球重点研究的技术之一，以应对全球气候变暖和减少二氧化碳向大气排放的问题。未来的研究需要针对这些技术和方法的难题和挑战进行研发攻关，以突破现阶段的瓶颈，推动二氧化碳捕集技术的经济性、高效性和规模化。
二氧化碳捕集技术是一种关键的碳减排技术，可以有效地减少二氧化碳的排放，减缓全球气候变暖的速度。近年来，随着全球对气候变化问题的关注加深，二氧化碳捕集技术的研究和应用得到了广泛的关注和快速的发展。现有的二氧化碳捕集技术大致包括燃烧前捕集、燃烧后捕集、富氧燃烧和化学链燃烧等几种技术路线。各种技术都有其优势和局限性，目前还没有一种技术能够独立满足高效、低成本、低能耗和大规模的要求。其中，燃烧后捕集是在燃料燃烧之后捕集二氧化碳。这种方法的优点是可以捕集燃烧过程中产生的二氧化碳，但可能需要较高的能耗和成本。常见的技术包括胺类吸收法、碳酸盐吸收法等。
现有技术中CN201510529951.2公开一种二氧化碳捕集系统，包括吸收塔具有：吸收塔第一入口，连通于风机出口；吸收塔第一出口，设置于吸收塔的顶部；吸收塔第二入口，设置于吸收塔的上部；以及吸收塔第二出口，设置于吸收塔的底部。该技术采用传统吸收塔，对碳钢+防腐层及合金吸收塔的维护维修工作代价逐年高昂；CN201910171708.6公开一种用于燃煤电厂二氧化碳捕集的循环预处理系统，包括水洗塔、设于水洗塔内部且自下而上分布的多个填料层本体、循环水冷却器、自动加碱装置以及盐度调节装置。该预处理系统，采用多个填料层本体组合的方式，将烟气中的灰尘、SO2等有害物质充分清除，提高了水洗效率，并达到降低烟气温度的目的；水洗塔外部设有自动加碱装置和盐度调节装置，能够根据循环洗涤水的pH设定值来自动调节加碱量，以有效地去除烟尘中的酸性物质含量，保证了烟气的水洗效果，并且可以根据循环洗涤水中的盐度自动补水，防止因盐度过高而结垢。烟气中，普遍含有氮氧化物，硫氧化物，粉尘，一般进入吸收塔需要对烟气进行预处理，该技术中采用水洗塔，存在传递效率不高，传质较差的缺陷。
发明内容
本发明的目的是为了克服现有技术存在的捕集成本高，大规模碳捕集吸收塔工程放大难的问题，提供一种二氧化碳捕集系统和方法及应用，具有低成本、低能耗的优势。
为了实现上述目的，本发明第一方面提供一种二氧化碳捕集系统，所述二氧化碳捕集系统包括：
预处理单元，用于去除含有二氧化碳的烟气中的粉尘，所述预处理单元包括旋流分离器，所述旋流分离器具有使水洗液呈雾状分布的液相进料件和使烟气形成旋流与水洗液接触的旋流结构；
吸收单元，与所述预处理单元的气相出口相连通，用于使二氧化碳吸收剂与烟气接触形成富液；
解吸单元，与所述吸收单元的富液出口相连通，用于使富液在超重力下进行解吸出二氧化碳并得到贫液；
热交换单元，用于收集所述解吸单元的出料热量。
本发明二方面提供一种二氧化碳捕集方法，在本发明的系统中进行，所述方法包括以下步骤：
1)将含有二氧化碳的烟气形成旋流，使水洗液分散分布且与旋流态的所述烟气接触以将烟气中的粉尘去除；
2)将步骤1)中处理后的所述烟气与二氧化碳吸收剂接触形成富液；
3)将步骤2)中的富液在超重力下解吸得到二氧化碳和贫液；
4)将步骤3)中的出料热量收集用于出口物料实现热量回收再利用。
本发明提供本发明的二氧化碳捕集方法和/或二氧化碳捕集系统在大于50万吨/年二氧化碳捕集中的应用。
通过上述技术方案，本发明的二氧化碳捕集系统采用超重力耦合热量收集技术，实现热量的综合利用，与传统解吸技术相比，解吸能耗可降低15-20％以上，在大规模碳捕集中可显著降低二氧化碳捕集成本。
本发明的二氧化碳捕集方法采用超重力解吸使富液破碎成液滴、液线和液膜，提高热质利用效率；结合热量收集技术，能够实现热量的综合利用，降低能耗；进一步地，采用混凝土吸收塔提高使用寿命，降低维修机率；在以大规模碳捕集中可显著降低二氧化碳捕集成本，具有高效、低成本、低能耗和大规模的优势。
附图说明
图1是本发明一些实施例的二氧化碳捕集系统的流程示意图；
图2是本发明一些实施例的旋流分离器的结构示意图；
图3是本发明一些实施例的混凝土吸收塔的结构示意图；
图4是本发明一些实施例的超重力解吸装置的结构示意图；
图5是本发明另一些实施例的超重力解吸装置的结构示意图；
图6是本发明一些实施例的移动床的结构示意图。
附图标记说明
1预处理单元；              1-1切向烟气进口；
1-2液相进料件；           1-3气相出口；
1-4液相出口；             2吸收单元；
2-1烟气进料口；            2-2二氧化碳吸收剂/贫液进料口；
2-3尾气出口；             2-4富液出口；
2-5填料单元；            3解吸单元；
3-1-1壳体；              3-1-2转轴；
3-1-3轴承；              3-1-4微波头；
3-1-5侧向贫液出口；       3-1-6侧向气体进口；
3-1-7富液进口；          3-1-8气体出口；
3-2-1进液口；            3-2-2进气口；
3-2-3出液口；            3-2-4出气口；
4贫液净化单元；         4-1移动架；
4-2净化罐；              5热交换单元。
具体实施方式
以下结合附图对本发明的具体实施方式进行详细说明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本发明，并不用于限制本发明。
在本文中所披露的范围的端点和任何值都不限于该精确的范围或值，这些范围或值应当理解为包含接近这些范围或值的值。对于数值范围来说，各个范围的端点值之间、各个范围的端点值和单独的点值之间，以及单独的点值之间可以彼此组合而得到一个或多个新的数值范围，这些数值范围应被视为在本文中具体公开。
在本发明中，在未作相反说明的情况下，使用的方位词如“上、下、顶、底”通常是针对附图所示的方向而言的或者是针对竖直、垂直或重力方向上而言的各部件相互位置关系描述用词，“内、外”通常指的是相对于腔室而言的腔室内外或相对于圆心而言的径向内外。
本发明公开一种二氧化碳捕集系统，如图1所示，该二氧化碳捕集系统包括：
预处理单元1，用于去除含有二氧化碳的烟气中的粉尘，所述预处理单元1包括旋流分离器，所述旋流分离器具有使水洗液呈雾状分布的液相进料件1-2和使烟气形成旋流与水洗液接触的旋流结构；
吸收单元2，与预处理单元1的气相出口相连通，用于使二氧化碳吸收剂与烟气接触形成富液；
解吸单元3，与吸收单元2的富液出口相连通，用于使富液在超重力下进行解吸出二氧化碳得到贫液；
热交换单元5，用于收集解吸单元3的出料热量。
本发明的二氧化碳捕集系统采用超重力耦合热量收集技术，实现热量的综合利用，与传统解吸技术相比，解吸能耗可降低15-20％以上，在大规模碳捕集中可显著降低二氧化碳捕集成本。
预处理单元1包括旋流分离器，如图2所示，旋流分离器的顶端设置有水洗液进料管，该水洗液进料管的出料端设有使分散分布的液相进料件1-2，旋流分离器中设置有使烟气形成旋流与水洗液接触的旋流结构。
本发明中对旋流结构无特殊要求，只要能够使烟气形成旋流与水洗液接触即可，在一些实施例中，旋流分离器设有横截面为圆形的腔体，旋流结构可以设置为开设在腔体的切向烟气进口1-1，通过使烟气在腔体的切向进料形成旋流。
本发明中对液相进料件1-2无特殊要求，只要能够使水洗液尽可能分散即可，在一些实施例中，液相进料件可以采用现有技术中的高速旋转钛金属圆盘结构。
在一些实施例中，旋流分离器可以设置在预处理塔中，旋流分离器的气相出口1-4连通预处理塔的顶端，旋流分离器的液相出口1-3可以通过水洗液循环管线连通液相进料件1-2，实现水洗液的循环利用。
在一些实施例中，吸收单元2包括混凝土吸收塔，如图1所示，混凝土吸收塔由上至下依次开设尾气出口2-3、二氧化碳吸收剂/贫液进料口2-2、烟气进料口2-1和富液出口2-4，其中，烟气进料口2-1连通预处理塔的顶端，使来自预处理单元1的烟气与二氧化碳吸收剂逆流接触，二氧化碳吸收剂可以来新鲜的二氧化碳吸收剂也可以为贫液，如图3所示，尾气出口2-3与二氧化碳吸收剂/贫液进料口2-2之间设置丝网除沫器，二氧化碳吸收剂/贫液进料口2-2与烟气进料口2-1之间沿高度方向间隔设有多个填料单元2-5，每个填料单元2-5由上至下依次设置有吸收剂分布器、填料层和集液器，其中，填料层采用规整填料，首个填料单元中的吸收剂分布器的进料端与二氧化碳吸收剂/贫液进料口2-2相连通，相邻两个填料单元中，上一个单元的集液器与下一个单元的吸收剂分布器的进料端相连通，每个填料单元中的吸收剂分布器的喷嘴采用现有技术中的雾化喷嘴，可以理解的是，雾化喷嘴的雾化程度越高越能够提高二氧化碳吸收剂和/或贫液的初始分散效率。
需要说明的是，在以胺液作为二氧化碳吸收剂的体系中，“解吸”是胺分子与CO2形成不稳定盐类在受热后(～100℃)发生分解反应，CO2从液相扩散至气相实现CO2分离和溶剂再生过程。受热分解反应是吸收过程的逆反应，对于构成混合胺的伯胺、仲胺、叔胺体系，反应动力学属于瞬时快速。因此，解吸反应动力学瞬时的特性，决定了CO2分子从液相到气相的气液传质过程速率是整个解吸反应-传质耦合过程的速度控制步骤。本发明中超重力技术对于该类过程能够强化传质效果，有效改善了传统塔器设备气液传质效率较低、反应器体积大的弱点。
在一些实施例中，解吸单元3包括超重力解吸装置，如图4所示，超重力解吸装置包括壳体3-1-1围绕限定的解吸腔，解吸腔中设有轴向延伸的转轴3-1-2，转轴3-1-2与壳体3-1-1通过轴承3-1-3连接，转轴3-1-2上设有沿轴向间隔排布的微波头3-1-4，壳体3-1-1的顶端开设有富液进口3-1-7、上部开设有侧向气体进口3-1-6，下部开设侧向贫液出口3-1-5，底部开设有气体出口3-1-8，壳体3-1-1的顶端安装电机，该电机通过电滑环与转轴连接，转轴上开设有用于安装线缆的线槽，通过线缆将微波头与电滑环电连接。具体地，电滑环的固定外环与外部电源连接，滑动内环与转轴3-1-2紧箍，内环电源通过线槽与转轴3-1-2固定，供电微波探头，随后富液从侧向富液进口进入，热氢气从侧向气体进口3-1-6进入，使转轴转速400-1500rpm，在微波存在下解吸富液，生成贫液从侧向贫液出口3-1-5出料，解吸的CO2从气体出口3-1-8排出。
本发明中，采用微波与转轴的耦合能够降低解吸温度与解吸能耗，在微波存在下实现富胺液热解吸，同时加速富胺液流体流动，提高热质传递效率，与传统蒸汽解吸相比，能够降低解吸能耗，缩短工艺流程，省去再沸器，减少与工艺工程蒸汽的工艺连接。
在一些实施例中，解吸单元3的超重力解吸装置不仅局限于图4所示，还可以采用CN 116328496 A公开的离心分散设备，如图5所示，该离心分散设备的壳体的顶端设置进液口3-2-1和出气口3-2-4，壳体的底端开设出液口3-2-3、壳体的侧面设置进气口3-2-2；当使用氢气对富液进行解吸时，进气口3-2-2连接氢气进料管线；当使用蒸汽解吸富液时，该离心分散设备的出液口3-2-3与进气口3-2-2连通且连通管路上设置再沸器，如此，贫液从出液口3-2-3出料进再沸器产生蒸汽通过进气口3-2-2进入。
以胺液作为二氧化碳吸收剂中，化学胺二氧化碳捕集工艺的60-70％能耗来自解吸过程，提高解吸过程效率将有效降低化学胺捕集工艺能耗与成本，为此，在一些实施例中，热交换单元可以采用现有技术中的热泵组件(例如型号为约克YHAP-C溴化锂的热泵组件)对解吸单元3的气体出口3-1-8或出气口3-2-4的出料的热量进行收集升温以对解吸单元3的解吸提供热量，如此，本发明通过超重力技术可将富液破碎成液滴、液线和液膜，提高热质利用效率，并结合热泵组件进一步地降低解吸过程中的能耗，对于大规模碳捕集(大于50万吨/年)，具有较低的工程成本的优势。
在一些实施例中，解吸单元3的贫液出口或出液口3-2-3与吸收单元2通过贫液管路相连通，将解吸后得到的贫液返回吸收单元与烟气接触吸收二氧化碳。
在一些实施例中，优选贫液管路上安装有贫液净化单元4，用于去除贫液中的热稳定性盐。
在一些实施例中，贫液净化单元4包括移动床，移动床包括至少一个床层，每个床层包括能够环绕移动床中心移动的移动架4-1，沿移动架长度方向间隔安装有多个净化罐4-2。具体的，如图6所示，移动架可以设置为圆形且能够旋转，沿该移动架周向间隔安装有6个净化罐4-2，使贫液依次进入各净化罐去除贫液中的热稳定性盐，本发明中移动床可以设置两个沿高度方向堆叠设置的床层，可以两个床层交替实现贫液净化。
在前述公开的基础上，本发明公开一种二氧化碳捕集方法，该方法在本发明的系统中进行，包括以下步骤：
1)将含有二氧化碳的烟气形成旋流，使水洗液分散分布且与旋流态的所述烟气接触以将烟气中的粉尘去除；
2)将步骤1)中处理后的烟气与二氧化碳吸收剂接触形成富液；
3)将步骤2)中的富液在超重力下解吸得到二氧化碳和贫液；
4)将步骤3)中的出料热量收集再利用。
本发明的二氧化碳捕集方法采用超重力耦合热量收集技术，实现热量的综合利用，与传统解吸技术相比，解吸能耗可降低15-20％以上，在大规模碳捕集中可显著降低二氧化碳捕集成本。
其中，使步骤1)中烟气形成旋流，使水洗液分散分布且与旋流态的烟气接触，需要说明的是，来自工业装置包括炼厂催化裂化装置、炼厂合成氨装置、炼厂制氢装置及电厂燃煤锅炉的烟气中，普遍含有氮氧化物，硫氧化物，粉尘等物质，现有技术中采用的水洗塔方式存在传递效率不高，传质较差的缺陷，特别是在大规模碳捕集中，该缺陷将被放大，本发明使烟气形成旋流，将水洗液破碎成液膜、液线和液滴，提高传质比表面积，可降低水洗液用量，提高处理效果。
本发明中对水洗液无特殊要求，例如可以为能够脱除硫氧化物的碱液也可以为水，碱液可以为常用的氢氧化钠水溶液均可用于本发明。
本发明中，烟气与二氧化碳吸收剂接触的条件的可选范围较宽，以下示范性说明，但不因此限制本发明的范围，针对本发明，步骤2)中烟气与二氧化碳吸收剂接触的条件包括：温度范围40-50℃，常压。
本发明中，常规二氧化碳吸收剂均适用于本发明，以下示范性说明，但不因此限制本发明的范围，在一些实施例中，二氧化碳吸收剂选自MDEA、MEA、AEEA、PZ中的至少一种。
需要说明的是，传统的吸收塔多为金属材质，例如碳钢+防腐层及合金吸收塔，但是这类吸收塔的维护维修工作代价逐年高昂，特别是应用于大规模捕集工艺中，维护维修代价更高，为此，在一些实施例中，使步骤2)中烟气与二氧化碳吸收剂在混凝土吸收塔中接触，相比于现有技术中的以金属材料为主的吸收塔，混凝土吸收塔在长达数十年的使用寿命周期内具有较低的维护和维修机率，具有抗火灾、持久耐用、综合低成本、可设计性强的优点，具有更好的综合效益。在吸收塔具有相同结构的前提下，混凝土塔吸收塔可以放置更多大型内构件。更重要的是，随着塔体大型化趋势，高数十米乃至百米以上的混凝土吸收塔在节省初始投资方面的优势逐渐突出。以大规模低浓度二氧化碳捕集为例，相比于现有技术中的金属材质的吸收塔，混凝土吸收塔能够显著降低二氧化碳捕集成本，且混凝土塔，可通过模具，现场一体化浇筑，克服大型塔器的施工难度；同时，基于防腐工艺，实现大规模碳捕集的长周期运转。
为提高混凝土吸收塔的使用寿命，在一些实施例中，混凝土吸收塔的塔内壁采用现有技术进行防腐处理形成防腐层，例如可以采用耐腐蚀砖、防腐胶通过复合镶嵌工艺，将壁面防腐和塔体结构合为一体。
需要说明的是，现有技术中富胺液的解吸主要是通过送入再生塔顶部，与底部逆流而上的热蒸汽接触，再生塔内部无法便捷的调控气液的接触状态，且往往存在传热不足的缺陷，为此，本发明采用超重力解吸，利用离心力使富液破碎提高热质利用效率，为降低解吸能耗，在一些实施例中，步骤3)中，在微波和超重力下对富液进行解吸，本发明采用微波和超重力结合的方式能够实现良好的解吸效果的同时降低解吸能耗。
在一些实施例中，含有二氧化碳的烟气中二氧化碳体积含量10-30％。
在一些实施例中，微波的频率为2450土50MHz。
在一些实施例中，超重力操作条件包括:转速400-1200rpm。
在一些实施例中，步骤3)中，可以采用热氢气和/或蒸汽对富液进行解吸。
为降低解吸过程中的潜热，在一些实施例中，优选采用热氢气对富液进行解吸，解吸后得到的氢气和二氧化碳还可以进一步地制备甲醇或低碳烯烃，更优选热氢气的温度为90-108℃。
在一些实施例中，热氢气与富液的体积流量比为30-60:1。
在一些实施例中，将步骤3)中的贫液返回步骤2)与来自步骤1)的烟气接触吸收二氧化碳，优选将步骤3)中的贫液净化后返回步骤2)与来自步骤1)的烟气接触吸收二氧化碳。
本发明中，对贫液进行连续净化无特殊要求，常用的净化剂均可用于本发明，以下示范性说明，但不因此限制本发明的范围，在一些实施例中，采用离子交换树脂对贫液进行连续净化。
本发明中，净化条件的可选范围较宽，以下示范性说明，但不因此限制本发明的范围，针对本发明，净化条件包括：常温常压。
在一些实施例中，步骤4)中，采用热泵收集步骤3)中出料热量。
本发明公开本发明的二氧化碳捕集方法和/或本发明的二氧化碳捕集系统在大于50万吨/年二氧化碳捕集中的应用。
以下将通过实施例来说明本发明的优势，但本发明并不仅局限于此，以下实施例中采用二氧化碳检测仪进行评价分析，捕集效率的计算方式为混凝土吸收塔出口二氧化碳浓度与入口二氧化碳浓度的比值，二氧化碳纯度的计算方式为解吸气二氧化碳含量与解吸气总含量的比值。混凝土吸收塔中混凝土强度达到C40，抗震等级7级。
实施例1
本实施例采用图1所示的二氧化碳捕集系统，包括：预处理单元1、吸收单元2、解吸单元3、贫液净化单元4和热交换单元5。
其中，预处理单元1包括旋流分离器，旋流分离器的顶端设置有水洗液进料管，该水洗液进料管的出料端设有高速旋转钛金属圆盘结构，旋流分离器的横截面为圆形的腔体，旋流结构设置为开设在腔体的切向烟气进口1-1。
吸收单元2包括混凝土吸收塔，混凝土吸收塔由上至下依次开设尾气出口2-3、二氧化碳吸收剂/贫液进料口2-2、烟气进料口2-1和富液出口2-4，其中，烟气进料口2-1连通预处理塔的顶端，尾气出口2-3与二氧化碳吸收剂/贫液进料口2-2之间设置丝网除沫器，二氧化碳吸收剂/贫液进料口2-2与烟气进料口2-1之间沿高度方向间隔设有多个填料单元2-5，每个填料单元2-5由上至下依次设置有吸收剂分布器、填料层和集液器，其中，首个填料单元中的吸收剂分布器的进料端与二氧化碳吸收剂/贫液进料口2-2相连通，相邻两个填料单元中，上一个单元的集液器与下一个单元的吸收剂分布器的进料端相连通。
解吸单元3采用图5所示的离心分散设备，该离心分散设备的壳体的顶端设置进液口3-2-1和出气口3-2-4，壳体的底端开设出液口3-2-3、壳体的侧面设置进气口3-2-2；该离心分散设备的出液口3-2-3与进气口3-2-2连通且连通管路上设置再沸器。
贫液净化单元4包括移动床，移动床包括2个床层，每个床层包括能够环绕移动床中心移动的圆形移动架4-1，沿该移动架周向间隔安装有6个净化罐4-2，解吸单元3的出液口3-2-3与二氧化碳吸收剂/贫液进料口2-2通过贫液管路相连通，贫液管路连通净化罐4-2。
热交换单元5包括约克YHAP-C溴化锂的热泵组件，约克YHAP-C溴化锂的热泵组件的热量输入管线连通出气口3-2-4，热量输出管线两端各自端连通出液口3-2-3和进液口3-2-1。
采用前述二氧化碳捕集系统处理来自电厂烟气(二氧化碳体积含量13.5％)，通入切向烟气进口1-1形成旋流，与通过高速旋转钛金属圆盘结构进料的水洗液接触预处理烟气降温至45℃且通过水洗除去粉尘颗粒，接触条件包括温度为45℃、压力为常压；随后预处理后的烟气进入混凝土吸收塔的烟气进料口2-1，混合胺水溶液(质量浓度以胺计35％)通过二氧化碳吸收剂/贫液进料口2-2进入混凝土吸收塔，胺液与二氧化碳逆流接触反应，捕集效率达98％，形成富胺液通过富液出口2-4进入超重力解吸单元3，解吸单元3采用图5所示的离心分散设备与来自再沸器的蒸汽(温度105℃)逆流接触，其中，离心分散设备的转速为450r/min，蒸汽与富胺液的进料体积流量比为50：1；富胺液发生解吸反应(解吸压力为常压)，变为贫胺液，贫胺液通贫液管路上的移动床通过离子交换树脂在常温常压条件下去除热稳定性盐后通过二氧化碳吸收剂/贫液进料口2-2返回混凝土塔；且解吸后的二氧化碳与贫胺液在热泵组件中进行换热，本实施例中，解吸能耗2.6GJ/t CO2，解吸后的二氧化碳纯度达到97％。
实施例2
与实施例1不同的是：采用前述二氧化碳捕集系统处理来自大庆石化催化裂化装置的烟气(二氧化碳体积含量30％)，通入切向烟气进口1-1形成旋流，与通过高速旋转钛金属圆盘结构进料的水洗液接触预处理烟气降温至45℃且通过水洗除去粉尘颗粒，接触条件包括温度为45℃、压力为常压；随后预处理后的烟气进入混凝土吸收塔的烟气进料口2-1，混合胺水溶液(质量浓度以胺计35％)通过二氧化碳吸收剂/贫液进料口2-2进入混凝土吸收塔，胺液与二氧化碳逆流接触反应，捕集效率达95％，形成富胺液通过富液出口2-4进入超重力解吸单元3，解吸单元3采用图5所示的离心分散设备与来自再沸器的蒸汽(温度105℃)逆流接触，其中，离心分散设备的转速为800r/min，蒸汽与富胺液的进料体积流量比为35：1；富胺液发生解吸反应(解吸压力为常压)，变为贫胺液，贫胺液通贫液管路上的移动床通过离子交换树脂在常温常压条件下去除热稳定性盐后通过二氧化碳吸收剂/贫液进料口2-2返回混凝土塔；且解吸后的二氧化碳与贫胺液在热泵组件中进行换热，本实施例中，解吸能耗2.63GJ/t CO2，解吸后的二氧化碳纯度达到96.5％。
实施例3
与实施例1不同的是：采用前述二氧化碳捕集系统处理来自大庆石化催化裂化装置的烟气(二氧化碳体积含量18％)，通入切向烟气进口1-1形成旋流，与通过高速旋转钛金属圆盘结构进料的水洗液接触预处理烟气降温至45℃且通过水洗除去粉尘颗粒，接触条件包括温度为45℃、压力为常压；随后预处理后的烟气进入混凝土吸收塔的烟气进料口2-1，混合胺水溶液(质量浓度以胺计35％)通过二氧化碳吸收剂/贫液进料口2-2进入混凝土吸收塔，胺液与二氧化碳逆流接触反应，捕集效率达97％，形成富胺液通过富液出口2-4进入超重力解吸单元3，解吸单元3采用图5所示的离心分散设备与来自再沸器的蒸汽(温度105℃)逆流接触，其中，离心分散设备的转速为1150r/min，蒸汽与富胺液的进料体积流量比为60：1；富胺液发生解吸反应(解吸压力为常压)，变为贫胺液，贫胺液通贫液管路上的移动床通过离子交换树脂在常温常压条件下去除热稳定性盐后通过二氧化碳吸收剂/贫液进料口2-2返回混凝土塔；且解吸后的二氧化碳与贫胺液在热泵组件中进行换热，本实施例中，解吸能耗可达到2.57GJ/t CO2，解吸后的二氧化碳纯度达到97.3％。
实施例4
与实施例1不同的是，解吸单元3采用图4所示的超重力解吸装置，该超重力解吸装置包括壳体3-1-1围绕限定的解吸腔，解吸腔中设有轴向延伸的转轴3-1-2，转轴3-1-2与壳体3-1-1通过轴承3-1-3连接，转轴3-1-2上设有沿轴向间隔排布的微波头3-1-4，壳体3-1-1的顶端开设有富液进口3-1-7、上部开设有侧向气体进口3-1-6，下部开设侧向贫液出口3-1-5，底部开设有气体出口3-1-8，壳体3-1-1的顶端安装电机，该电机通过电滑环与转轴连接，转轴上开设有用于安装线缆的线槽，通过线缆将微波头与电滑环电连接。该超重力解吸装置的富液进口3-1-7连通富液出口2-4，超重力解吸装置的侧向气体进口3-1-6通入热氢气，贫液出口3-1-5与二氧化碳吸收剂/贫液进料口2-2通过贫液管路相连通，贫液管路连通净化罐4-2，热交换单元5包括约克YHAP-C溴化锂的热泵组件，约克YHAP-C溴化锂的热泵组件的热量输入管线连通气体出口3-1-8，热量输出管线两端各自端连通解吸腔。
其中，转轴3-1-2转速800rpm，微波头3-1-4频率为2450MHz，侧向气体进口3-1-6进入的热氢气(温度95℃)与富液进口3-1-7进入的富胺液的体积流量比为50：1。
结果：与实施例1相比，解吸温度降低10℃，蒸发潜热降低10％，解吸能耗达1.9GJ/t CO2，解吸后的二氧化碳纯度达到98.7％。
实施例5
与实施例1不同的是，解吸单元3采用图4所示的超重力解吸装置，该超重力解吸装置包括壳体3-1-1围绕限定的解吸腔，解吸腔中设有轴向延伸的转轴3-1-2，转轴3-1-2与壳体3-1-1通过轴承3-1-3连接，转轴3-1-2上设有沿轴向间隔排布的微波头3-1-4，壳体3-1-1的顶端开设有富液进口3-1-7、上部开设有侧向气体进口3-1-6，下部开设侧向贫液出口3-1-5，底部开设有气体出口3-1-8，壳体3-1-1的顶端安装电机，该电机通过电滑环与转轴连接，转轴上开设有用于安装线缆的线槽，通过线缆将微波头与电滑环电连接。该超重力解吸装置的富液进口3-1-7连通富液出口2-4，超重力解吸装置的侧向气体进口3-1-6通入热氢气，贫液出口3-1-5与二氧化碳吸收剂/贫液进料口2-2通过贫液管路相连通，贫液管路连通净化罐4-2，热交换单元5包括约克YHAP-C溴化锂的热泵组件，约克YHAP-C溴化锂的热泵组件的热量输入管线连通气体出口3-1-8，热量输出管线两端各自端连通解吸腔。
其中，不启动微波，转轴3-1-2转速800rpm，侧向气体进口3-1-6进入的热氢气(温度105℃)与富液进口3-1-7进入的富胺液的体积流量比为50：1。
结果：与实施例1相比，解吸温度不变，蒸发潜热降低10％，解吸能耗达2.3GJ/t CO2，解吸后的二氧化碳纯度达到98.2％。
实施例6
与实施例1不同的是，针对二氧化碳捕集系统处理来自大庆石化催化裂化装置的烟气(二氧化碳体积含量12％)，解吸单元3不设置再沸器，离心分散设备接入来自工艺工程管网的热氢，与富胺液逆流接触，氢气与富胺液的进料体积流量比为45：1。
结果：与实施例1相比，解吸温度不变，蒸发潜热降低12％，解吸能耗达2.2GJ/t CO2，解吸后的二氧化碳纯度达到98.0％。
实施例7
与实施例1不同的是，解吸单元3采用图4所示的超重力解吸装置，该超重力解吸装置包括壳体3-1-1围绕限定的解吸腔，解吸腔中设有轴向延伸的转轴3-1-2，转轴3-1-2与壳体3-1-1通过轴承3-1-3连接，转轴3-1-2上设有沿轴向间隔排布的微波头3-1-4，壳体3-1-1的顶端开设有富液进口3-1-7、上部开设有侧向气体进口3-1-6，下部开设侧向贫液出口3-1-5，底部开设有气体出口3-1-8，壳体3-1-1的顶端安装电机，该电机通过电滑环与转轴连接，转轴上开设有用于安装线缆的线槽，通过线缆将微波头与电滑环电连接。该超重力解吸装置的富液进口3-1-7连通富液出口2-4，超重力解吸装置的侧向气体进口3-1-6通入蒸汽，贫液出口3-1-5与二氧化碳吸收剂/贫液进料口2-2通过贫液管路相连通，贫液管路连通净化罐4-2，热交换单元5包括约克YHAP-C溴化锂的热泵组件，约克YHAP-C溴化锂的热泵组件的热量输入管线连通气体出口3-1-8，热量输出管线两端各自端连通解吸腔。
其中，转轴3-1-2转速800rpm，微波头3-1-4频率为2450MHz，侧向气体进口3-1-6进入的蒸汽(温度95℃)与富液进口3-1-7进入的富胺液的体积流量比为50：1。
结果：与实施例1相比，解吸温度不变，蒸发潜热降低2％，解吸能耗达2.43GJ/t CO2，解吸后的二氧化碳纯度达到98.3％。
对比例1
与实施例1不同的是，解吸单元采用现有技术中的同处理量的再生塔进行解吸。
结果：解吸能耗达2.8GJ/t CO2。
以上结合附图详细描述了本发明的优选实施方式，但是，本发明并不限于此。在本发明的技术构思范围内，可以对本发明的技术方案进行多种简单变型，包括各个具体技术特征以任何合适的方式进行组合，为了避免不必要的重复，本发明对各种可能的组合方式不再另行说明。但这些简单变型和组合同样应当视为本发明所公开的内容，均属于本发明的保护范围。

Claims (19)

  1. 一种二氧化碳捕集系统，其特征在于，所述二氧化碳捕集系统包括：
    预处理单元(1)，用于去除含有二氧化碳的烟气中的粉尘，所述预处理单元(1)包括旋流分离器，所述旋流分离器具有使水洗液呈雾状分布的液相进料件(1-2)和使烟气形成旋流与水洗液接触的旋流结构；
    吸收单元(2)，与所述预处理单元(1)的气相出口相连通，用于使二氧化碳吸收剂与烟气接触形成富液；
    解吸单元(3)，与所述吸收单元(2)的富液出口相连，用于使富液在超重力下进行解吸出二氧化碳并得到贫液；
    热交换单元(5)，用于收集所述解吸单元(3)的出料热量。
  2. 根据权利要求1所述的二氧化碳捕集系统，其特征在于，所述旋流分离器具有横截面为圆形的腔体，所述旋流结构设置为开设在所述腔体的切向烟气进口(1-1)。
  3. 根据权利要求1或2所述的二氧化碳捕集系统，其特征在于，吸收单元(2)包括混凝土吸收塔，所述混凝土吸收塔的塔内壁设有防腐层。
  4. 根据权利要求3所述的二氧化碳捕集系统，其特征在于，所述混凝土吸收塔中沿高度方向间隔设有多个填料单元(2-5)，每个所述填料单元(2-5)由上至下依次设置有吸收剂分布器、填料层和集液器。
  5. 根据权利要求1所述的二氧化碳捕集系统，其特征在于，解吸单元(3)包括超重力解吸装置，所述超重力解吸装置包括壳体(3-1-1)围绕限定的解吸腔，所述解吸腔中设有轴向延伸的转轴(3-1-2)，所述转轴(3-1-2)与所述壳体(3-1-1)通过轴承(3-1-3)连接，所述转轴(3-1-2)上设有沿轴向间隔排布的微波头(3-1-4)，所述壳体(3-1-1)的顶端开设有富液进口(3-1-7)、上部开设有侧向气体进口(3-1-6)、下部开设侧向贫液出口(3-1-5)、底部开设有气体出口(3-1-8)。
  6. 根据权利要求1或5所述的二氧化碳捕集系统，其特征在于，解吸单元(3)的贫液出口与吸收单元(2)通过贫液管路相连通。
  7. 根据权利要求6所述的二氧化碳捕集系统，其特征在于，所述贫液管路上安装有贫液净化单元(4)，用于去除所述贫液中的热稳定性盐。
  8. 根据权利要求7所述的二氧化碳捕集系统，其特征在于，贫液净化单元(4)包括移动床，所述移动床包括至少一个床层，每个所述床层包括能够环绕所述移动床中心移动的移动架(4-1)，沿所述移动架长度方向间隔安装有多个净化罐(4-2)。
  9. 一种二氧化碳捕集方法，其特征在于，该方法采用权利要求1-8中任意一项所述的系统，包括以下步骤：
    1)使含有二氧化碳的烟气形成旋流，使水洗液分散分布且与旋流态的所述烟气接触以将烟气中的粉尘去除；
    2)将步骤1)处理后的烟气与二氧化碳吸收剂接触形成富液；
    3)将步骤2)中的富液在超重力下解吸得到二氧化碳和贫液；
    4)将步骤3)中的出料热量收集。
  10. 根据权利要求9所述的方法，其特征在于，步骤1)中含有二氧化碳的烟气中二氧化碳体积含量10-30％。
  11. 根据权利要求9或10所述的方法，其特征在于，使步骤2)中烟气与二氧化碳吸收剂在混凝土吸收塔中接触，所述混凝土吸收塔的塔内壁设有防腐层。
  12. 根据权利要求9所述的方法，其特征在于，步骤4)中采用热泵收集出料热量。
  13. 根据权利要求9所述的方法，其特征在于，步骤3)中，在微波和超重力下对富液进行解吸。
  14. 根据权利要求13所述的方法，其特征在于，所述微波的频率为2450土50MHz；和/或
    超重力操作条件包括：转速400-1200rpm。
  15. 根据权利要求9所述的方法，其特征在于，步骤3)中，采用热氢气和/或蒸汽作为气源对富液进行解吸。
  16. 根据权利要求15所述的方法，其特征在于，采用热氢气作为气源对富液进行解吸，热氢气的温度为90-108℃；和/或
    所述热氢气与富液的体积流量比为30-60:1。
  17. 根据权利要求9所述的方法，其特征在于，该方法还包括：将步骤3)中的贫液返回步骤2)或者将步骤3)中的贫液净化后返回步骤2)。
  18. 根据权利要求17所述的方法，其特征在于，采用离子交换树脂对所述贫液进行连续净化。
  19. 权利要求1-8中任意一项所述的二氧化碳捕集系统和/或权利要求9-18中任意一项所述二氧化碳捕集方法在大于50万吨/年二氧化碳捕集中的应用。
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