CN215463249U - Partitioned multistage circulating CO2Trapping concentration system - Google Patents
Partitioned multistage circulating CO2Trapping concentration system Download PDFInfo
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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Abstract
本实用新型涉及一种分区多级循环CO2捕集浓缩系统，包括分区多级循环吸收塔、贫富液换热器、CO2再生塔、CO2浓缩装置，分区多级循环吸收塔、贫富液换热器、CO2再生塔和CO2浓缩装置顺次连通，所述分区多级循环吸收塔包括顺次连通的预洗涤装置、1～n‑1级CO2吸收段和n级水洗段，n≥3；1～n‑1级CO2吸收段和n级水洗段自下而上逐级串联在吸收塔内。本实用新型采用分区多级循环吸收塔，在发挥其CO2捕集效率高的优点的同时，大幅度提高二氧化碳的吸收容量；采用的多级循环自下而上依次进行气溶胶脱除、提高碳捕集效率、维持吸收速率和富液浓缩，降低了碳减排成本。
The utility model relates to a partitioned multi-stage circulating CO2 capture and concentration system, comprising a partitioned multistage circulating absorption tower, a lean-rich liquid heat exchanger, a CO2 regeneration tower, a CO2 concentration device, a partitioned multistage circulating absorption tower, a lean-rich liquid heat exchanger, a The rich liquid heat exchanger, the CO 2 regeneration tower and the CO 2 concentration device are connected in sequence, and the zoned multi-stage circulating absorption tower includes a pre-washing device, a 1-n-1 stage CO 2 absorption section and an n-stage water washing which are connected in sequence. stage, n≥3; 1-n-1 stage CO 2 absorption section and n-stage water washing section are connected in series in the absorption tower from bottom to top. The utility model adopts a partitioned multi-stage circulating absorption tower, which greatly improves the absorption capacity of carbon dioxide while exerting the advantages of high CO 2 capture efficiency; Carbon capture efficiency, maintenance of absorption rates, and enrichment of rich liquids reduce carbon abatement costs.
Description
Technical Field
The utility model belongs to the technical field of atmospheric pollution treatment and carbon emission reduction, and particularly relates to partitioned multistage circulating CO2A capture concentration system.
Background
Carbon dioxide is one of the main components of greenhouse gases causing global warming, and is mainly derived from the combustion of fossil fuels such as coal, oil, and natural gas. However, the carbon emission of coal-fired units and industrial production is large, and the overall smoke discharge property is represented as follows: the flue gas amount is large, the carbon dioxide content in the flue gas is low, the partial pressure is low, and the carbon dioxide trapping cost is high; the flue gas contains SO2、SO3、NOxHeavy metal and smoke dust, and other impurities, which are easy to generate secondary pollutants to CO2The trapping process has a certain negative impact. At present, the requirement for carbon emission reduction is higher and higher, and the main technical means for carbon emission reduction are CCS (carbon capture and sequestration) and CCUS (carbon capture, sequestration and utilization). The carbon capture technology is explored in China, a large carbon capture demonstration project is provided in the petrochemical industry and the chemical industry, and the tail gas is used for capturing carbon dioxide for chemical industry, oil displacement, geological storage or biological carbon fixation. The power industry has also built a number of carbon capture demonstration projects, either long term shut down or occasional operation after commissioning for a variety of reasons including high system operating costs, difficult product trips, etc. In the capturing, conveying, utilizing and sealing links of the CCUS technology, capturing is a link with large energy consumption and cost. The current low concentration capture cost in China is 300-600 yuan/t (CO)2). The post-combustion trapping technology is a widely applied MEA chemical absorption method, and the operation energy consumption can reach 4.0-6.0 MJ/kg CO2This will reduce the thermal efficiency of coal fired power plants by 25% to 40%. The investment and operation costs are too high, the energy consumption is large, and the urgent requirements of the CCUS are difficult to meet, so that the development of a post-combustion trapping technology with low energy consumption and low cost is urgent.
Chinese patent CN 102784546A designs a CO2The trapping system includes two-stage absorption tower comprising two sections of lower semi-lean liquid section and upper lean liquid section connected vertically in series, bottom rich liquid is made to enter normal pressure desorption tower for normal pressure desorptionThe liquid outlet at the bottom of the absorption tower is connected with the liquid inlet at the upper part of the semi-barren liquid section of the two-section absorption tower, the liquid outlet at the bottom of the atmospheric desorption tower is also connected with the liquid inlet at the top of the desorption tower, and the desorption tower is connected with a reboiler. The utility model improves CO by a semi-barren solution method2The capture rate is improved by combining normal pressure desorption and solution desorption2And (4) recovering rate. However, this technique has the following disadvantages: the absorption liquid is sent into the desorption tower without being absorbed to saturation in the semi-barren solution section, and the flow rate of the absorption liquid which is not added and enters the desorption tower is large, so that the desorption energy consumption is large; secondary pollutants such as aerosol are not controlled.
Chinese patent CN 109745850 a designed a pretreatment system for carbon dioxide capture in coal fired power plants. The system comprises: the water washing tower, a plurality of packing layer bodies which are arranged in the water washing tower and distributed from bottom to top, a circulating water cooler, an automatic alkali adding device and a salinity adjusting device. The system adopts a mode of combining a plurality of packing layer bodies to remove dust and SO in the flue gas2And the like. The automatic alkali adding device and the salinity adjusting device arranged outside the water washing tower can effectively remove the content of acidic substances in the smoke dust. However, this technique has the following disadvantages: the water washing tower and the gathering tower are separately arranged, the investment and operation cost is high, and CO is generated2The trapping efficiency is further improved with great difficulty, the desorption energy consumption is great, the adjustable range of the system operation parameters is small, and the adjustable performance is poor.
In order to reduce the high cost of the separation operation of the existing flue gas purification system and the carbon capture system, the development of a novel absorbent with high absorption rate, large absorption capacity and low desorption energy consumption is the most effective method, but a large amount of experiments are required for accumulation due to large technical difficulty.
Therefore, in order to overcome the defects in the prior art, research on CO with low cost, stability, high efficiency and high capture rate is needed2A capture concentration system.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects of the prior art, the utility model provides a partitioned multistage circulation CO2A capture concentration system; the advantage of high carbon capture efficiency is exerted, and each section of circulating CO is regulated and controlled in a partitioning and grading manner2The absorption process is as followsThe absorption process and the desorption process are adjusted in a segmented manner, so that the trapping energy consumption is greatly reduced, and the process flow is convenient and easy to operate.
The technical scheme adopted by the utility model is as follows:
partitioned multistage circulating CO2A capture concentration system, the CO2The capture concentration system comprises a partitioned multistage circulating absorption tower (CO)2Absorption tower), lean-rich liquid heat exchanger and CO2Regeneration column, CO2Concentration device, partitioned multistage circulating absorption tower, lean and rich liquid heat exchanger and CO2Regeneration column and CO2The concentrating devices are communicated in sequence, and the partitioned multistage circulating absorption tower comprises a prewashing device and 1-n-1 stage CO which are communicated in sequence2An absorption section and an n-stage water washing section, wherein n is more than or equal to 3; 1-n-1 grade CO2The absorption section and the n-stage water washing section are connected in series in the absorption tower from bottom to top.
Preferably, the CO is2The trapping and concentrating system also comprises an intelligent control system which is respectively connected with the 1-n-1 grade CO2The absorption section is connected with the n-stage water washing section.
Preferably, the pre-washing device is a venturi type pre-washing section or a vertical type pre-washing tower.
The prewashing device washes, removes impurities and reduces the temperature of water to softened water, adopts the high-efficient spray nozzle to spray, washes, removes impurities and reduces the temperature of water and recycles, discharges to the wet flue gas desulfurization slurrying system as slurrying water regularly.
The pre-washing device is arranged at the outlet (50-65 ℃) of the wet desulphurization tower and CO2The temperature of the section between the inlets of the absorption tower is 50-65 ℃, which is not beneficial to CO2The absorption amount of the absorption liquid is more at high temperature; the flue gas also contains fly ash, gypsum particles and SO2、SO3HCl, NOx and the like, while strongly acidic gases will preferentially CO2The water reacts with the absorption liquid to generate stable salts which are difficult to decompose and regenerate, so that the performance of the absorption liquid is rapidly reduced; aiming at the problems, the utility model is suitable for the pre-washing device for trapping the carbon in the discharged smoke of the coal-fired unit, reduces the loss of the absorption liquid in the absorption process, simultaneously inhibits the transfer of impurities in the smoke to the absorption liquid, and ensures that the absorption liquid can be efficiently circulatedThe use of the system reduces the operation cost and solves the problems of abnormal operation of the trapping system and the like caused by improper pretreatment.
Taking an n-stage circulating absorption tower (n is 4) provided with a Venturi pre-washing section as an example, a pre-washing device is the Venturi pre-washing section, and the circulating absorption tower is a four-stage circulating absorption tower with n being 4; preferably, the multistage circulating absorption tower comprises a Venturi prewashing section and a first stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2An absorption section and a four-stage water washing section, first-stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section and the four-stage water washing section are connected in series from bottom to top step by step, and the Venturi pre-washing section and the one-stage CO are connected in series2The absorption section is connected.
Partitioned multistage circulating CO of four-stage circulating absorption tower2When the trapping concentration system is used, the method comprises the following steps:
(1) high-temperature flue gas enters a four-stage circulating absorption tower, is removed of impurity ions through a Venturi pre-washing section arranged at the front part and is cooled, and then enters a first-stage CO sequentially2Absorption stage, secondary CO2Absorption stage, three-stage CO2An absorption section and a four-stage water washing section;
wherein, the first stage CO2The absorption section is an absorbent circulation, the pH value is 7.7-9.0, and the temperature is 49-60 ℃;
two stage CO2The absorption section is an absorbent circulation, the pH value is 8.0-10.0, and the temperature is 44-53 ℃;
three stage CO2The absorption section is an absorbent circulation, the pH value is 9.5-11.5, and the temperature is 40-48 ℃;
the four-stage washing section is a softened water circulation, the pH value is 8.5-10.0, and the temperature is 40-48 ℃;
(2) heating the rich solution to 90-98 ℃ by a lean-rich solution heat exchanger, and introducing the heated rich solution into CO2In the desorption tower, after the absorption liquid is heated to 105-115 ℃, the lean liquid is discharged with CO2The desorption tower enters a lean and rich liquid heat exchanger to be cooled to 60-68 ℃, enters a cleaning device and then enters three-stage CO2An absorption section;
(3)CO2introducing the regenerated steam of the desorption tower into CO2A concentration device cooled to the temperature by a coolerCO2Enters a gas-liquid separator below the boiling point to obtain high-purity CO2；
(4) The intelligent control system is respectively connected with the first-level CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section is connected with the four-stage water washing section, and the partitioned multi-stage circulating CO is established based on key parameters including pH, temperature and circulating amount of each stage2The absorption system global optimization parameter model realizes stable, efficient and low-cost operation of the system.
CO2The drag weights of the absorber tower are different at different heights, CO2The resistance analysis of the absorption tower at different tower heights is shown in fig. 1, and the gas phase diffusion resistance gradually increases and the liquid phase reaction resistance gradually decreases with the increase of the tower height. At low CO level in the absorption tower2The absorption rate is limited by the resistance to liquid phase reaction and the CO can be increased by increasing the slurry residence time2The amount of absorption; the three resistances are relatively average in the middle of the absorption tower, the total absorption resistance is small and is CO2A primary force absorbing section; high CO in the absorption tower2The absorption rate is limited by gas phase diffusion resistance, and the gas-liquid two-phase concentration gradient can be increased by increasing the pH value of the absorbent, so that the decarburization efficiency is improved. The utility model provides a partitioned multistage circulation CO based on mass transfer-reaction regulation and control by a mode of multistage decarburization and one-stage water washing according to the theoretical design2A capture concentration system.
Preferably, the primary CO2The absorption section comprises a section of packing layer, a section of nozzle, a first clapboard and a first air lifting cap which are sequentially arranged from bottom to top, and the bottom of the absorption tower is communicated with the section of nozzle through a liquid enrichment pump and a section of circulating cooler;
two stage CO2The absorption section comprises a second section packing layer, a second section nozzle, a second clapboard and a second air lifting cap which are sequentially arranged from bottom to top, the bottom of the absorption section is communicated with a second section circulation tank, and the second section circulation tank is communicated with the second section nozzle through a second section circulating pump and a second section circulating cooler;
three stage CO2The absorption section comprises three sections of packing layers, three sections of nozzles, a third clapboard and a third air lifting cap which are sequentially arranged from bottom to top, the bottom of the absorption section is communicated with three sections of circulation grooves, and three sections of circulation grooves are communicatedThe tank is communicated with the three-section nozzles through a three-section circulating pump and a three-section circulating cooler;
the four-stage water washing section comprises a four-stage packing layer and four-stage nozzles which are sequentially arranged from bottom to top, the bottom of the four-stage water washing section is communicated with a four-stage circulation tank, and the four-stage circulation tank is communicated with the four-stage nozzles through a four-stage circulation pump and a four-stage circulation cooler.
Preferably, a first demister for removing aerosol and liquid drops is arranged in the multistage circulating absorption tower, and the first demister is positioned above the n-stage water washing section.
Preferably, the first-section nozzle, the second-section nozzle, the third-section nozzle and the fourth-section nozzle are any one of an Archimedes spiral structure nozzle, a bidirectional hollow cone nozzle or a unidirectional hollow cone nozzle;
further preferably, when the first-stage nozzle, the second-stage nozzle and the third-stage nozzle are in Archimedes spiral shapes, 32 nozzles are circumferentially arranged, and the nozzles are small-particle-size 5-head nozzles with the aperture of 0.8 mm. The spraying device adopts a small-particle-size multi-head nozzle for high-density spraying, and the circular tube has an Archimedes spiral structure, so that the spraying device has the advantages of compact structure, high atomization degree, strong universality and the like, realizes the homogenization of liquid, and meets the requirements in practical application.
For CO2The problems of absorbent loss and secondary pollutant generation caused by aerosol generated in the absorption process are solved, and the four-section nozzle is preferably a high-efficiency atomized one-way hollow cone nozzle or a two-way hollow cone nozzle by combining the environmental characteristics in the absorption tower, so that fine particles of the original flue gas are removed, and entrainment of fine-particle-size absorption liquid is inhibited. The influence characteristics of parameters such as flue gas supersaturation degree, temperature drop and residence time on the condensation growth of supersaturated water vapor, escape absorbent and the like are combined, the association between the flue gas flow field structure at the top of the absorption tower and the collision coalescence characteristics of particles, organic amine aerosol and fog drops is analyzed, a turbulent flow field is arranged between a first demister and a four-stage water washing section to form a turbulent flow field to promote the collision coalescence of the organic amine aerosol and the fog drops, and then pollutants such as the organic amine aerosol and the like are removed efficiently.
Preferably, the CO is2The desorption tower comprises a desorption heater, a desorption tower nozzle and a desorption towerA tower packing layer, a desorption tower lift cap and a desorption tower clapboard; desorption tower partition, desorption heater and CO2The bottoms of the desorption towers are communicated; CO22The second demister is arranged at the top of the desorption tower.
The desorption heating heat source is extracted from a steam turbine intermediate pressure cylinder.
Preferably, the CO is2The concentration device comprises a cooler, a gas-liquid separator, a CO separator2The top of the desorption tower forms a circulation.
Preferably, a slurry cleaning device is arranged at the downstream of the lean liquid section of the lean-rich liquid heat exchanger; the slurry cleaning device comprises an ion exchanger and a filter. A slurry cleaning device is additionally arranged to prevent the system from scaling and the absorbent from degrading; the barren solution enters an ion exchanger in the slurry cleaning device, metal ions in the absorption solution are removed by adopting ion exchange resin, the barren solution can be repeatedly regenerated and used, the service life is long, and the operating cost is low; and then enters a filter in a slurry cleaning device to remove insoluble impurities in the absorption liquid.
The lean-rich liquid heat exchanger is used for connecting a multistage circulating absorption tower and CO2The desorption tower is connected. First stage CO2The rich solution in the absorption section enters the lean-rich solution heat exchanger through a rich solution pump for heat exchange and then exchanges heat with CO2The upper part of the desorption tower is communicated with the desorption tower nozzle. CO22The barren solution at the bottom of the desorption tower enters a barren and rich solution heat exchanger through a barren solution pump for heat exchange, enters a slurry cleaning device, is communicated with a three-section circulating cooler, and enters a three-stage CO2An absorption section.
The cooling water of the first-stage circulating cooler, the second-stage circulating cooler, the third-stage circulating cooler and the fourth-stage circulating cooler comes from a demineralized water tank, and the cooling water after heat exchange supplements the water supply of a heat supply boiler.
The utility model recycles the waste heat of the cold water, and the cooling water after heat exchange supplements the water supply of the heat supply boiler, thereby improving the economic benefit of the power plant.
The utility model has the beneficial effects that: adopts a partitioned multistage circulating absorption tower to exert CO thereof2The carbon dioxide collecting device has the advantage of high collecting efficiency, and greatly improves the absorption capacity of carbon dioxide; n stages of cycles from bottom to topThe aerosol removal, the carbon capture efficiency improvement, the absorption rate maintenance and the rich liquid concentration are sequentially carried out, the absorption section and the desorption section are respectively regulated, and the carbon capture rate can reach more than 99 percent; effectively reduces CO while reducing the flow of absorption liquid entering the desorption tower2The desorption energy consumption and the overall desorption energy consumption are not higher than 2.2GJ/tCO2The trapping cost is reduced by more than 10%.
Drawings
FIG. 1 shows CO2Schematic resistance analysis diagrams of absorption towers at different tower heights;
FIG. 2 is a three-stage recycle process flow diagram;
FIG. 3 is a control schematic diagram of the intelligent regulation system;
FIG. 4 is a schematic view of the structure of an Archimedes spiral structured nozzle;
FIG. 5 is a three stage cycle process flow diagram with a venturi pre-wash section;
FIG. 6 is a four stage cycle process flow diagram with a venturi pre-wash section;
FIG. 7 is a four-stage recycle process flow diagram with a prewash column.
Detailed Description
The present invention will be further described with reference to the following specific examples, but the scope of the present invention is not limited thereto. Those skilled in the art can and should understand that any simple changes or substitutions based on the spirit of the present invention should fall within the protection scope of the present invention.
Example 1
Referring to FIG. 2, a zoned multistage recycle CO2A capture concentration system, the CO2The capture concentration system comprises a multistage circulating absorption tower 15, a lean-rich liquid heat exchanger 21, a slurry cleaning device 22 and CO2Desorption column 31 and CO2And (4) a concentration device.
The multistage circulating absorption tower 15 includes a first stage CO2Absorption stage, secondary CO2An absorption section and a third-stage water washing section; first stage CO2Absorption stage, secondary CO2The absorption section and the three-stage water washing section are connected in series from bottom to top step by step, and the first demisting is arranged at the top of the multi-stage circulating absorption tower 15Device 11-1.
The flue gas enters first-stage CO2The absorption section sequentially passes through a section of packing layer 4, a section of nozzle 3, a first clapboard 2 and a first air lifting cap 1, and the decarburization efficiency is 35%; absorbent in first-stage CO2Circulating in the absorption section, controlling the pH at 8.0 and the temperature at 52 ℃; the absorbent overflowing from the second section circulation tank 17 is injected into the slurry tank 32, enters the multistage circulation absorption tower 15 through the rich liquid pump 16, the first section circulation cooler 12 and the first section nozzle 3, has a liquid-gas ratio of 0.86, and falls into the slurry tank 32 after reversely contacting with the flue gas through the first section packing layer 4. After the liquid level of the slurry tank 32 reaches a certain height, the saturated rich solution enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 and then enters the CO2 A desorption column 31.
The flue gas enters secondary CO2The absorption section sequentially passes through a second section packing layer 8, a second section nozzle 7, a second clapboard 6 and a second air lifting cap 5, and the decarburization efficiency is 85%; absorbent in secondary CO2Circulating in the absorption section, controlling the pH at 9.3 and the temperature at 46 ℃; the absorbent overflowing from the three-section circulation tank 2-19 is injected into the two-section circulation tank 2-17, enters the multistage circulation absorption tower 15 through the two-section circulation pump 18, the two-section circulation cooler 13 and the two-section nozzle 7, has a liquid-gas ratio of 1.3, falls onto the first partition plate 2 after being in reverse contact with the flue gas through the two-section packing layer 8, and then flows to the two-section circulation tank 17. The liquid level of the second-stage circulation tank 17 reaches a certain height and then overflows to the second-stage slurry tank 32.
The flue gas enters a three-stage washing section, sequentially passes through a three-stage packing layer 10 and three-stage nozzles 9, the aerosol removal efficiency is over 95 percent, and the flue gas is discharged to the atmosphere after passing through a first demister 11-1; the softened water circulates in the third-stage water washing section, the pH is controlled at 9.2, and the temperature is 41 ℃; fresh softened water is injected into the three-section circulating tank 19, enters the multistage circulating absorption tower 15 through the three-section circulating pump 20, the three-section circulating cooler 14 and the three-section nozzle 9, has the liquid-gas ratio of 0.6, falls to the second partition plate 6 after being in reverse contact with flue gas through the three-section packing layer 10, and flows back to the three-section circulating tank 19.
Referring to fig. 3, the intelligent regulation system is respectively connected with the primary CO2Absorption section (first stage circulation), second stage CO2The absorption section (second-stage circulation) is connected with the third-stage water washing section (third-stage circulation), and the desorption energy consumption and CO are adjusted according to the real-time operation parameters2Collecting efficiency of constructionAnd (4) optimizing the model, and adjusting the operation parameters to be optimal in real time. The intelligent control system receives signals from a slurry pool 32, a pregnant solution pump 16, a two-stage circulation tank 17, a two-stage circulation pump 18, a three-stage circulation tank 19 and a three-stage circulation pump 20. The method comprises the following steps:
establishing a database covering parameters such as multi-equipment multi-scale inlet and outlet flue gas parameters, reaction liquid parameters, desorption energy consumption and the like based on-line monitoring and off-line data and equipment design parameters, wherein the parameters include but are not limited to flue gas flow G and CO at a flue gas inlet and outlet2Partial pressure
And
concentration of absorbent cabpH, temperature T and circulation quantity L of 1-n stages of circulating liquid;
secondly, obtaining the relation between desorption energy consumption and pH value, temperature and circulation quantity of each level based on mechanism research and parameter database, and constructing the partitioned multistage circulation CO2An absorption-desorption process multi-factor regulation and control key parameter model driven by the capture and concentration system mechanism and data in a cooperative mode is researched, meanwhile, efficiency-energy consumption-material consumption key indexes in a partition multistage circulation running state are researched, and partition multistage circulation CO is constructed2A comprehensive cost model of energy consumption-material consumption of the trapping concentration system;
an absorption-desorption process multi-factor regulation key parameter model:
energy consumption-material consumption comprehensive cost model:
thirdly, establishing a partition under variable load/working condition of efficiency-energy consumption-material consumption analysis by utilizing the established absorption-desorption mechanism and data cooperative driving model and the energy consumption-material consumption comprehensive cost modelMulti-stage cycle CO2Overall optimization parameter model of trapping and concentrating system for real-time and accurate evaluation of CO under different working conditions2Trapping the dynamic running cost of the whole absorption-desorption process of the concentration system, and establishing the partitioned multi-stage circulation CO2The method comprises the following steps of collecting the cost-effectiveness optimization problem of a concentration system, and solving through intelligent optimization algorithms such as particle swarm optimization and ant colony optimization to obtain a parameter combination with optimal energy consumption and material consumption comprehensive cost;
zoned multi-stage recycle of CO2The cost-effectiveness optimization problem of the trapping concentration system is as follows:
fourthly, after a parameter combination with optimal energy consumption-material consumption comprehensive cost is obtained, the parameter combination is taken as a control target, advanced control methods such as predictive control and fuzzy control are adopted, real-time, accurate and stable control of the parameters is realized, and CO is ensured2The efficiency of the trapping concentration system stably reaches the standard and simultaneously realizes the optimal energy consumption and material consumption.
Referring to fig. 4, the first-stage, second-stage and third-stage nozzles are of Archimedes spiral structures, the circular tube 4-1 is of an Archimedes spiral shape, 32 nozzles 4-2 are circumferentially arranged, the nozzles 4-2 are small-particle-size 5-head nozzles, and the aperture is 0.8 mm. The small-particle-size multi-head nozzle is adopted for high-density spraying, so that the device has the advantages of compact structure, high atomization degree, strong universality and the like, realizes the homogenization of liquid, and meets the requirements in practical application. The four-section nozzle adopts a single-phase hollow cone nozzle.
The cooling water of the first-stage circulating cooler, the second-stage circulating cooler and the third-stage circulating cooler comes from a demineralized water tank, and the cooling water after heat exchange supplements the water supply of the heat supply boiler.
The rich solution is heated to 97 ℃ by a lean-rich solution heat exchanger 21 and then enters CO2The desorption tower 31 falls into the desorption tower clapboard 27 through the desorption tower nozzle 24 and the desorption tower filler layer 25 and circulates to the desorption towerA heater 28. After the absorption liquid is heated to 107 ℃, the lean solution is subjected to CO discharge2The desorption tower 31 enters the lean-rich liquid heat exchanger 21 to be cooled to 63 ℃. High temperature CO enrichment2Steam enters a desorption tower packing layer 25 through a desorption tower gas lifting cap 26 and enters CO through a second demister 11-22A concentration device; the heat source of the desorption heater 28 is 180 ℃ air exhaust from a steam turbine intermediate pressure cylinder, and the temperature is reduced to 128 ℃ and returned to the water tank.
CO2The regenerated steam of the desorption tower 31 enters CO2A concentration device, which is cooled to CO by a cooler 292Enters a gas-liquid separator 30 below the boiling point to obtain high-purity CO2。
The lean-rich liquid heat exchanger 21 is used for circulating the absorption tower 15 and CO in multiple stages2The desorption tower 31 is connected. First stage CO2The rich solution in the absorption section enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 for heat exchange, and then exchanges heat with CO2The upper stripper nozzles 24 of the stripper 31 are connected. CO22The barren liquor at the bottom of the desorption tower 31 enters the barren liquor heat exchanger 21 through the barren liquor pump 23 for heat exchange, enters the slurry cleaning device 22, is communicated with the two-stage circulating cooler 13, and enters the secondary CO2An absorption section.
The slurry washing device 22 is arranged downstream of the lean section of the lean-rich liquid heat exchanger 21, and includes an ion exchanger and a filter. The barren solution enters an ion exchanger in the slurry cleaning device, metal ions in the absorption solution are removed by adopting ion exchange resin, the barren solution can be repeatedly regenerated and used, the service life is long, and the operating cost is low; and then enters a filter in a slurry cleaning device to remove insoluble impurities in the absorption liquid.
5000m3After the flue gas with the volume of the flue gas per hour is treated by the system, the decarburization efficiency is 95%. The desorption energy consumption is less than 2.2GJ/t CO2。
Example 2
Referring to FIG. 5, a zoned multistage recycle CO2A capture concentration system, the CO2The capture concentration system comprises a multistage circulating absorption tower 15, a lean-rich liquid heat exchanger 21, a slurry cleaning device 22 and CO2Desorption column 31 and CO2And (4) a concentration device.
The multistage circulating absorption tower 15 bagsIncluding a Venturi prewash stage 33, a first stage CO2An absorption section, a secondary CO2 absorption section and a tertiary water washing system. First stage CO2Absorption stage, secondary CO2The absorption section and the three-stage water washing section are connected in series from bottom to top step by step, and the first demister 11 is arranged at the top of the multi-stage circulating absorption tower 15.
The Venturi type pre-washing section 33 is arranged at the front part of the multistage circulating absorption tower 15 and is connected with the first-stage CO2The absorption section is communicated, the washing, impurity removal and cooling water of the pre-washing section is preferably softened water, the softened water is sprayed by a high-efficiency atomizing nozzle 34, the washing, impurity removal and cooling water is recycled and is periodically discharged to a wet desulphurization pulping system to be used as pulping water.
The flue gas enters a Venturi pre-washing section 33 and is cooled to 42 ℃.
The flue gas enters first-stage CO2The absorption section sequentially passes through a section of packing layer 4, a section of nozzle 3, a first clapboard 3-2 and a first air lifting cap 1, and the decarburization efficiency is 39%; absorbent in first-stage CO2Circulating in the absorption section, controlling the pH at 8.0 and the temperature at 52 ℃; the absorbent overflowing from the second section circulation tank 17 is injected into the slurry tank 32, enters the multistage circulation absorption tower 15 through the rich liquid pump 16, the first section circulation cooler 12 and the first section nozzle 3, has a liquid-gas ratio of 0.86, and falls into the slurry tank 32 after reversely contacting with the flue gas through the first section packing layer 4. After the liquid level of the slurry tank 32 reaches a certain height, the saturated rich solution enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 and then enters the CO2 A desorption column 31.
The flue gas enters secondary CO2The absorption section sequentially passes through a second section packing layer 8, a second section nozzle 7, a second clapboard 6 and a second air lifting cap 5, and the decarburization efficiency is 89%; absorbent in secondary CO2Circulating in the absorption section, controlling the pH at 9.3 and the temperature at 46 ℃; the absorbent overflowing from the three-section circulation tank 19 is injected into the two-section circulation tank 17, enters the multistage circulation absorption tower 15 through the two-section circulation pump 18, the two-section circulation cooler 13 and the two-section nozzle 7, has a liquid-gas ratio of 1.3, falls onto the first partition plate 2 after being in reverse contact with the flue gas through the two-section packing layer 8, and then flows back to the two-section circulation tank 17. The liquid level of the second-stage circulation tank 17 reaches a certain height and then overflows to the second-stage slurry tank 32.
The flue gas enters a three-stage washing section, sequentially passes through a three-stage packing layer 10 and three-stage nozzles 9, the aerosol removal efficiency is over 97 percent, and the flue gas is discharged to the atmosphere after passing through a first demister 11-1; the softened water circulates in a three-stage washing system, the pH is controlled at 9.2, and the temperature is 41 ℃; fresh softened water is injected into the three-section circulating tank 19, enters the multistage circulating absorption tower 15 through the three-section circulating pump 20, the three-section circulating cooler 14 and the three-section nozzle 9, has the liquid-gas ratio of 0.6, falls to the second partition plate 6 after being in reverse contact with flue gas through the three-section packing layer 10, and flows back to the three-section circulating tank 19.
Referring to fig. 3, the intelligent regulation system is respectively connected with the primary CO2Absorption stage, secondary CO2The absorption section is connected with a three-stage water washing system, and the desorption energy consumption and CO are determined according to real-time operation parameters2And modeling optimization is carried out on the trapping efficiency, and the operation parameters are adjusted to be optimal in real time. The intelligent control system receives signals from a slurry pool 32, a pregnant solution pump 16, a two-stage circulation tank 17, a two-stage circulation pump 18, a three-stage circulation tank 19 and a three-stage circulation pump 20.
The cooling water of the first-stage circulating cooler, the second-stage circulating cooler and the third-stage circulating cooler comes from a demineralized water tank, and the cooling water after heat exchange supplements the water supply of the heat supply boiler.
The lean-rich liquid heat exchanger 21 is used for circulating the absorption tower 15 and CO in multiple stages2The desorption tower 31 is connected. First stage CO2The rich solution in the absorption section enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 for heat exchange, and then exchanges heat with CO2The upper stripper nozzles 24 of the stripper 31 are connected. CO22The barren liquor at the bottom of the desorption tower 31 enters the barren liquor heat exchanger 21 through the barren liquor pump 23 for heat exchange, enters the slurry cleaning device, is communicated with the two-stage circulating cooler 13, and enters the second-stage CO2An absorption section.
Other embodiments refer to example 1.
5000m3After the flue gas with the volume of the flue gas per hour is treated by the system, the decarburization efficiency is 97%; the desorption energy consumption is less than 2.2GJ/t CO2。
Example 3
Referring to FIG. 6, a zoned multistage recycle CO2A capture concentration system, the CO2The capture concentration system comprises a multistage circulating absorption tower 15, a lean-rich liquid heat exchanger 21, a slurry cleaning device 22 and CO2Desorption column 31 and CO2And (4) a concentration device.
The multistage circulating absorption tower 15 comprises a Venturi type pre-washing section 33, a first stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2An absorption section and a four-stage water washing section. First stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section and the four-stage water washing section are connected in series from bottom to top step by step, and a first demister 11-1 is arranged at the uppermost part of the multistage circulating absorption tower 15.
The Venturi type pre-washing section 33 is arranged at the front part of the multistage circulating absorption tower 15 and is connected with the first-stage CO2The absorption section is communicated, the washing, impurity removal and cooling water of the pre-washing section is preferably softened water, the softened water is sprayed by a high-efficiency atomizing nozzle 34, the washing, impurity removal and cooling water is recycled and is periodically discharged to a wet desulphurization pulping system to be used as pulping water.
The flue gas enters a Venturi pre-washing section 33 and is cooled to 38 ℃.
The flue gas enters first-stage CO2The absorption section sequentially passes through a section of packing layer 4, a section of nozzle 3, a first clapboard 2 and a first air lifting cap 1, and the decarburization efficiency is 40%; absorbent in first-stage CO2Circulating in the absorption section, controlling the pH at 8.5 and the temperature at 52 ℃; the absorbent overflowing from the second section circulation tank 17 is injected into the slurry tank 32, enters the multistage circulation absorption tower 15 through the rich liquid pump 16, the first section circulation cooler 12 and the first section nozzle 3, has a liquid-gas ratio of 0.86, and falls into the slurry tank 32 after reversely contacting with the flue gas through the first section packing layer 4. After the liquid level of the slurry tank 32 reaches a certain height, the saturated rich solution enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 and then enters the CO2 A desorption column 31.
The flue gas enters secondary CO2The absorption section sequentially passes through a second section packing layer 8, a second section nozzle 7, a second clapboard 6 and a second air lifting cap 5, and the decarburization efficiency is 90%; absorbent in secondary CO2Circulating in the absorption section, controlling the pH at 9.3 and the temperature at 46 ℃; the absorbent overflowing from the three-section circulation tank 19 is injected into the two-section circulation tank 17, enters the multistage circulation absorption tower 15 through the two-section circulation pump 18, the two-section circulation cooler 13 and the two-section nozzle 7, has a liquid-gas ratio of 1.3, falls onto the first partition plate 2 after being in reverse contact with the flue gas through the two-section packing layer 8, and then flows back to the two-section circulation tank 17. Two-stage circulation tank 17The liquid level overflows to the stage slurry tank 32 after reaching a certain height.
Flue gas enters three-stage CO2The absorption section sequentially passes through three sections of packing layers 42, three sections of nozzles 41, a third clapboard 40 and a third air lifting cap 39, and the decarburization efficiency is 98%; absorbent in tertiary CO2Circulating in the absorption section, controlling the pH at 10.2 and the temperature at 41 ℃; injecting fresh absorbent into the three-section circulation tank 19, entering the multistage circulation absorption tower 15 through the three-section circulation pump 20, the three-section circulation cooler 35 and the three-section nozzle 41, enabling the liquid-gas ratio to be 1.1, enabling the fresh absorbent to fall onto the second partition plate 6 after being in reverse contact with the flue gas through the three-section filler layer 42, and circulating the fresh absorbent to the three-section circulation tank 19; the third-stage circulating bath solution 19 overflows to the second-stage circulating bath 17 after reaching a certain height.
The flue gas enters a four-stage water washing section, sequentially passes through a four-stage packing layer 44 and four-stage nozzles 43, the aerosol removal efficiency is over 99 percent, and the flue gas is discharged to the atmosphere after passing through a first demister 11-1; softened water circulates in a four-stage water washing section, the pH is controlled at 9.2, and the temperature is 41 ℃; fresh softened water is injected into the four-section circulating tank-37, enters the multistage circulating absorption tower 15 through the four-section circulating pump 38, the four-section circulating cooler 36 and the four-section nozzle 43, has a liquid-gas ratio of 0.6, falls onto the third partition plate 40 after being in reverse contact with flue gas through the four-section packing layer 44, and then flows to the four-section circulating tank 37.
Referring to fig. 3, the intelligent regulation system is respectively connected with the primary CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section is connected with the four-stage water washing section, and the desorption energy consumption and CO are adjusted according to the real-time operation parameters2And modeling optimization is carried out on the trapping efficiency, and the operation parameters are adjusted to be optimal in real time. The intelligent control system receives signals from a slurry pool 32, a pregnant solution pump 16, a two-section circulating tank 17, a two-section circulating pump 18, a three-section circulating tank 19, a three-section circulating pump 20, a four-section circulating tank 37 and a four-section circulating pump 38.
The cooling water of the first-stage circulating cooler, the second-stage circulating cooler, the third-stage circulating cooler and the fourth-stage circulating cooler comes from a demineralized water tank, and the cooling water after heat exchange supplements the water supply of the heat supply boiler.
The lean-rich liquid heat exchanger 21 is used for circulating the absorption tower 15 and CO in multiple stages2The desorption tower 31 is connected. First stage CO2The rich solution in the absorption section enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 for heat exchange, and then exchanges heat with CO2The upper stripper nozzles 24 of the stripper 31 are connected. CO22The barren liquor at the bottom of the desorption tower 31 enters the barren liquor heat exchanger 21 through the barren liquor pump 23 for heat exchange, enters the slurry cleaning device, is communicated with the three-section circulating cooler-35, and enters the three-stage CO2An absorption section.
Other embodiments refer to example 1.
5000m3After the smoke with the smoke volume/h is treated by the system, the decarburization efficiency is 99%; the desorption energy consumption is less than 2.2GJ/t CO2。
Example 4
Referring to FIG. 7, a zoned multistage recycle CO2Capture concentration process system, said CO2The capture concentration system comprises a pre-washing tower 45, a multi-stage circulating absorption tower 15, a lean and rich liquid heat exchanger 21, a slurry cleaning device 22 and CO2Desorption column 31 and CO2And (4) a concentration device.
The multistage circulating absorption tower comprises a first stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2An absorption section and a four-stage water washing section. First stage CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section and the four-stage water washing section are connected in series from bottom to top step by step, and a first demister 11-1 is arranged at the top of the multi-stage circulating absorption tower.
The prewashing tower 45 is arranged at the front part of the multistage circulating absorption tower, washing, impurity removing and cooling water of the prewashing tower is preferably softened water, the softened water is sprayed by a high-efficiency atomizing nozzle 46, the washing, impurity removing and cooling water is recycled and is periodically discharged to a wet desulphurization pulping system 47 to be used as pulping water.
The flue gas enters a pre-washing tower 45 and is cooled to 40 ℃.
The flue gas enters first-stage CO2The absorption section sequentially passes through a section of packing layer 4, a section of nozzle 3, a first clapboard 2 and a first air lifting cap 1, and the decarburization efficiency is 41%; absorbent in first-stage CO2Circulating in the absorption section, controlling the pH at 9.0 and the temperature at 52 ℃; the absorbent overflowing from the two-stage circulation tank 17 is injected into a slurry tank 32 and enters a plurality of slurry tanks through a rich liquid pump 16, a one-stage circulation cooler 12 and a one-stage nozzle 3The liquid-gas ratio of the stage circulation absorption tower is 0.86, and the stage circulation absorption tower falls into the slurry pool 32 after being in reverse contact with the flue gas through the section of packing layer 4. After the liquid level of the slurry tank 32 reaches a certain height, the saturated rich solution enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 and then enters the CO2 A desorption column 31.
The flue gas enters secondary CO2The absorption section sequentially passes through a second section packing layer 8, a second section nozzle 7 and a second clapboard 6, and the decarburization efficiency is 91%; absorbent in secondary CO2Circulating in the absorption section, controlling the pH at 9.3 and the temperature at 46 ℃; the absorbent overflowing from the three-section circulation tank 19 is injected into the two-section circulation tank 17, enters the multistage circulation absorption tower through the two-section circulation pump 18, the two-section circulation cooler 13 and the two-section nozzle 7, has a liquid-gas ratio of 1.3, falls onto the first partition plate 2 after being in reverse contact with the flue gas through the two-section packing layer 8, and then flows back to the two-section circulation tank 17. The liquid level of the second-stage circulation tank 17 reaches a certain height and then overflows to the second-stage slurry tank 32.
Flue gas enters three-stage CO2The absorption section sequentially passes through three sections of packing layers 42, three sections of nozzles 41 and a third clapboard 40, and the decarburization efficiency is 98%; absorbent in tertiary CO2Circulating in the absorption section, controlling the pH at 10.2 and the temperature at 41 ℃; injecting fresh absorbent into the three-section circulation tank 19, entering the multistage circulation absorption tower 15 through the three-section circulation pump 20, the three-section circulation cooler 35 and the three-section nozzle 41, enabling the liquid-gas ratio to be 1.1, enabling the fresh absorbent to fall onto the second partition plate 6 after being in reverse contact with the flue gas through the three-section filler layer 42, and circulating the fresh absorbent to the three-section circulation tank 19; the third-stage circulating bath solution 19 overflows to the second-stage circulating bath 17 after reaching a certain height.
The flue gas enters a four-stage water washing section, sequentially passes through a four-stage packing layer 44 and four-stage nozzles 43, the aerosol removal efficiency is over 99 percent, and the flue gas is discharged to the atmosphere after passing through a first demister 11-1; softened water circulates in a four-stage water washing section, the pH is controlled at 9.2, and the temperature is 41 ℃; fresh softened water is injected into the four-section circulating tank 37, enters the multistage circulating absorption tower 15 through the four-section circulating pump 38, the four-section circulating cooler 36 and the four-section nozzle 43, has a liquid-gas ratio of 0.6, falls onto the third partition plate 40 after being in reverse contact with flue gas through the four-section packing layer 44, and is circulated to the four-section circulating tank 37.
Referring to fig. 3, the intelligent regulation system is respectively connected with the primary CO2Absorption stage, secondary CO2Absorption stage, three-stage CO2The absorption section is connected with the four-stage water washing section, and the desorption energy consumption and CO are adjusted according to the real-time operation parameters2And modeling optimization is carried out on the trapping efficiency, and the operation parameters are adjusted to be optimal in real time. The intelligent control system receives signals from a slurry pool 32, a pregnant solution pump 16, a two-section circulating tank 17, a two-section circulating pump 18, a three-section circulating tank 19, a three-section circulating pump 20, a four-section circulating tank 37 and a four-section circulating pump 38.
The cooling water of the first-stage circulating cooler, the second-stage circulating cooler, the third-stage circulating cooler and the fourth-stage circulating cooler comes from a demineralized water tank, and the cooling water after heat exchange supplements the water supply of the heat supply boiler.
The lean-rich liquid heat exchanger 21 is used for circulating the absorption tower and CO in multiple stages2The desorption tower 31 is connected. First stage CO2The rich solution in the absorption section enters the lean-rich solution heat exchanger 21 through the rich solution pump 16 for heat exchange, and then exchanges heat with CO2The upper stripper nozzles 24 of the stripper 31 are connected. CO22The lean solution at the bottom of the desorption tower 31 enters the lean-rich solution heat exchanger 21 through the lean solution pump 23 for heat exchange, enters the slurry cleaning device, is communicated with the three-section circulating cooler 35, and enters the three-stage CO2 absorption section.
Other embodiments refer to example 3.
5000m3After the smoke with the smoke volume/h is treated by the system, the decarburization efficiency is 99%; the desorption energy consumption is less than 2.2GJ/t CO2。
The utility model can collect CO with low energy consumption and high efficiency2And inhibit the generation of secondary pollutants while recovering high-purity CO2. CO in industry2Capture process, CO2The high energy consumption for trapping is the biggest problem of carbon trapping, and the existence of pollutants such as acid gas and metal ions can also cause CO2Trapping has an adverse effect. The non-circulating carbon trapping has high operation cost and large absorbent loss, so that the optimization target is stable and high-efficiency with low cost and low energy consumption by adopting multi-component means such as multi-stage circulating absorption, intelligent multi-factor regulation, pre-washing cooling, interstage cooling, post-stage washing, slurry cleaning, cooling water waste heat utilization, small-particle-size high-density spraying and the like, and the CO is subjected to CO capture2The generation of secondary pollutants is inhibited while the high-efficiency capture is carried out, and the CO is realized2Low energy consumption desorption and high purity concentration. The utility model adopts multi-stage decarburization and one-stage water washing in the absorption section of the partitioned multi-stage circulating absorption tower, so that different circulating sections can play different roles; low grade CO2The absorption section can increase the retention time of the absorbent and further improve CO2A load; middle grade CO2The absorption section is a main absorption section which absorbs CO at most2(ii) a High grade CO2The pH value of the absorption section is more than 10, so that the decarburization efficiency is ensured; the n-stage water washing section is softened water circulation and mainly aims at removing aerosol in the smoke and inhibiting generation of secondary pollutants. Different functions are combined together in the mode, so that the absorption tower is compact in structure and integrated in function, and a foundation is laid for further optimizing the layout of the flue gas purification system.
The utility model adopts multi-component means of multi-stage circulating absorption, intelligent multi-factor regulation, prewashing cooling, interstage cooling, after-stage water washing, slurry cleaning, cooling water waste heat utilization, small-particle-size high-density spraying and the like, takes low cost, low energy consumption, stability and high efficiency as an optimization target, and realizes CO purification2Effectively inhibit the generation of secondary pollutants while efficiently trapping, and realize CO2High efficiency capture, low energy consumption desorption and high purity concentration. The adopted multi-stage circulation sequentially carries out aerosol removal from top to bottom, improves carbon capture efficiency, maintains absorption rate and pregnant solution concentration, and improves the economic benefit of a power plant.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the utility model, many simple modifications can be made to the technical solution of the utility model, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the utility model, and all fall within the scope of the utility model.
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| WO2024011887A1 (en) * | 2022-07-14 | 2024-01-18 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide absorption system |
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| CN114712989A (en) * | 2022-03-11 | 2022-07-08 | 浙江大学 | Low-cost and high-efficiency co-adsorption-desorption decoupling method for pollutants and CO2 |
| CN114712989B (en) * | 2022-03-11 | 2023-01-03 | 浙江大学 | Low cost and high efficiency of pollutants and CO 2 Synergistic absorption-desorption decoupling method |
| WO2024011887A1 (en) * | 2022-07-14 | 2024-01-18 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide absorption system |
| CN116036842A (en) * | 2023-01-16 | 2023-05-02 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide trapping method |
| GB2635178A (en) * | 2023-11-01 | 2025-05-07 | Equinor Low Carbon Uk Ltd | Improvements to Absorber for Direct Air CO2 capture |
| CN119425278A (en) * | 2025-01-07 | 2025-02-14 | 安徽鑫纪源科技有限公司 | A pre-purification system for flue gas based on high-temperature oxygen-free pyrolysis of lithium batteries |
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