CN103274406A - Novel carbon dioxide trapping device performing liquefaction and then sublimation - Google Patents
Novel carbon dioxide trapping device performing liquefaction and then sublimation Download PDFInfo
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- CN103274406A CN103274406A CN2013102346669A CN201310234666A CN103274406A CN 103274406 A CN103274406 A CN 103274406A CN 2013102346669 A CN2013102346669 A CN 2013102346669A CN 201310234666 A CN201310234666 A CN 201310234666A CN 103274406 A CN103274406 A CN 103274406A
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Abstract
The invention discloses a novel carbon dioxide trapping device performing liquefaction and then sublimation. According to the device, research on physical properties of carbon dioxide and related mixtures is combined, and gas-liquid separation is performed firstly through a low temperature mode to obtain a part of liquid carbon dioxide; mixed gas after the liquefaction separating is cooled continuously and passes through two sublimation separating towers, and then carbon dioxide is separated; and dry ice obtained from sublimation separation is collected into a condensation pool, and the pressure is controlled above triple point pressure of carbon dioxide, so that the obtained dry ice can be melted directly into liquid carbon dioxide. The overall system design facilitates sufficient cold quantity recovery. The device improves the carbon dioxide trapping purity effectively, increases the carbon dioxide trapping efficiency, improves the cold quantity recovery rate of the system, and is energy-saving and low in consumption.
Description
Technical field
The present invention will be rich in the unstripped gas of carbonic acid gas by isolating carbonic acid gas for compression, the type of cooling, belong to refrigeration and low temperature technique field.
Background technology
When industrial development process is fast brought convenient life to people, also bring huge environmental problem to people, according to the USDOE statistics, the annual carbonic acid gas that discharges because of combustion of fossil fuels reaches more than 30,000,000,000 tons, but also in continuous growth.Heavy industry such as the power station of combustion of fossil fuels, oil factory, Steel Plant are main sources of Carbon emission, the carbonic acid gas volume content is about about 15% in the flue gas of power plant emission, the carbonic acid gas volume content is about about 35% than power plant's height in some Metallurgical Factory's discharged flue gas.In the flue gas that power plant, metallurgy industry burning mineral fuel produce, contain the great amount of carbon dioxide, also contain a certain amount of carbonic acid gas in undressed biogas and the Sweet natural gas, carbon dioxide content is between 5% to 98% in the gas material, thereby the quality of biogas and Sweet natural gas is exerted an influence.
On the other hand, carbonic acid gas is a kind of very valuable resource, has higher civilian and industrial value, now has been widely used in departments such as foodstuffs industry, chemical industry, mechanical industry, agricultural, commerce, transportation, oil production, national defence, fire-fighting.Comprise that mainly physics utilization and chemistry utilize: the Main physical purposes of carbonic acid gas comprises for the manufacture of the extraction agent of additive, fire-fighting medium, spices and the medicine of dry ice, supercritical extraction solvent, beverage and beer, clean-out system, is used for tobacco expanding, replaces Chlorofluorocarbons (CFCs) as whipping agent, gaseous fertilizer and is used for strengthening oil production (EOR) etc.; It mainly is to be that raw material can be produced multiple organic and inorganic chemical product with the carbonic acid gas that its chemistry is used, and in chemical industry, what utilize carbonic acid gas on a large scale mainly is urea, soda ash and bicarbonate of ammonia.
At the control problem of Carbon emission, both at home and abroad the insider has carried out long-term exploration, and to control the most direct effective means that carbonic acid gas increases in a short time be the capture of carrying out carbonic acid gas and seal up for safekeeping.Wherein mainly comprise solution absorption method, pressure swing adsorption process, membrane separation process etc.The solution absorption method technology maturation, use comparatively extensive, but this method is owing to the regeneration stage needs a large amount of heats to cause energy consumption bigger, the preparation absorption agent needs a large amount of energy consumptions and absorption agent to have corrodibility and toxicity, absorption agent can lose efficacy in the process of carrying out absorption and regeneration repeatedly simultaneously, needs constantly to replenish; Pressure swing adsorption process non-corrosiveness medium, running maintenance expense are low, but for obtaining higher carbon dioxide purity, need be than multiple adsorption tower, equipment control is difficulty comparatively, invests higher; The membrane separation process technological process is simple, and is easy to operate, but its to unstripped gas have relatively high expectations, present stage its treatment capacity little, filming technology is complicated, membrane stability is poor.Also there is common problem in above common method, namely separates the CO 2 that obtains and is gas, and requiring the expenditure of energy further is processed into liquid so that transportation is sealed up for safekeeping.In addition, separate the CO 2 purity of catching and generally be difficult to reach direct applied specification, the Carbon Dioxide Application after will catching if desired then needs further purification in each industry.
Summary of the invention
Goal of the invention: the objective of the invention is in order to overcome the deficiencies in the prior art, the novel carbon dioxide capture device that a kind of liquefaction is sublimated has again been proposed, the collecting carbonic anhydride that this device is primarily aimed in the high carbonated gas mixture separates, and improves the capture purity of carbonic acid gas, the capture rate of increase carbonic acid gas.
Technical scheme: in order to solve the problems of the technologies described above, the present invention adopts following technical scheme:
The novel carbon dioxide capture device that a kind of liquefaction is sublimated again, it has comprised the strainer, adsorber, moisture eliminator, first interchanger, compressor and second interchanger that connect successively; The outlet of described second interchanger is connected with No. three unstripped gas entrances of the 3rd interchanger, the interface of the 3rd interchanger also comprises No. three unstripped gas outlets, described No. three unstripped gass outlet is connected with the entrance of the 4th interchanger, and the outlet of the 4th interchanger is connected with No. five unstripped gas entrances of the 5th interchanger; The interface of described the 5th interchanger also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and described No. five unstripped gass outlet is connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower; The interface of described gas-liquid separation tower has also comprised the outlet of gas-liquid separation tower carbonic acid gas and has reclaimed the gas inlet, described gas-liquid separation tower carbonic acid gas outlet is connected with a pump intake, No. one pump outlet is connected with the rectifying tower carbonic acid gas entrance of rectifying tower, the interface of described rectifying tower also comprises the outlet of rectifying tower carbonic acid gas and the outlet of rectifying tower overhead gas, the outlet of rectifying tower overhead gas is reclaimed entrance with the gas-liquid separation tower and is connected, the outlet of rectifying tower carbonic acid gas is connected with No. five liquid carbon dioxide entrances, No. five liquid carbon dioxide outlets are connected with No. two pump intakes, and No. two pump outlet is connected with reservoir.
Wherein, the interface of described the 3rd interchanger also comprises No. three nitrogen separation entrances and No. three nitrogen separation gas outlets; The interface of described gas-liquid separation tower also comprises gas-liquid separation tower nitrogen outlet, gas-liquid separation tower nitrogen inlet and gas-liquid knockout tower mixed gas outlet; Wherein, No. three nitrogen separation entrances are connected with gas-liquid separation tower nitrogen outlet; The gas-liquid separation tower mixed gas outlet of described gas-liquid separation tower is connected with the knockout tower gas mixture entrance of sublimating of the knockout tower of sublimating, the interface of the described knockout tower of sublimating also comprises the knockout tower nitrogen inlet of sublimating No. one, the knockout tower nitrogen outlet of sublimating for No. one, the knockout tower carbonic acid gas of sublimating for No. one outlet and the knockout tower mixed gas outlet of sublimating for No., the described knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, the knockout tower nitrogen inlet of sublimating for No. one is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers of sublimating, the knockout tower carbonic acid gas of sublimating for No. one outlet is connected with No. five Liquid carbon dioxide entrances, the interface of described No. two knockout towers of sublimating has also comprised the knockout tower gas mixture entrance of sublimating No. two, the knockout tower mixed gas outlet of sublimating for No. two, the knockout tower carbonic acid gas of sublimating for No. two outlet and the knockout tower nitrogen inlet of sublimating for No. two, the knockout tower mixed gas outlet of wherein sublimating for No. one is connected with No. two knockout tower gas mixture entrances of sublimating, the knockout tower carbonic acid gas of sublimating for No. two outlet is connected with No. five Liquid carbon dioxide entrances, the knockout tower mixed gas outlet of sublimating for No. two is connected with the entrance of decompressor, and the outlet of decompressor is connected with No. two knockout tower nitrogen inlets of sublimating.
Wherein, described No. five unstripped gass outlet is connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower by the condensation pond of pipeline through sublimate knockout tower and No. two knockout towers of sublimating.
Wherein, described decompressor is cryogenic turboexpander.
Wherein, the refrigeration equipment of described sublimate knockout tower and No. two knockout towers of sublimating is the cascade refrigeration machine.
Wherein, sublimate for No. one heat exchanger surface of knockout tower and the knockout tower inside of sublimating for No. two is respectively equipped with electronic revolving scraper.
The present invention at first successively by strainer, adsorber and moisture eliminator, makes unstripped gas just carry out drying, purification earlier before capturing carbon dioxide gas unstripped gas.Native system does not adopt the solvent of chemical reactions such as hydramine, has avoided problems such as the corrodibility of the generation of toxic substance and equipment is serious.Then pass through repeatedly interchanger subzero treatment, unstripped gas is isolated liquid carbon dioxide by the gas-liquid separation tower, can directly lay in, continuation cooling is afterwards sublimated and is isolated dry ice.By the gas of sublimate knockout tower and the knockout tower after separating of sublimating for No. two, the content that wherein contains carbonic acid gas is lower, guarantees not produce the dry ice damage equipment, reclaims cold and work of expansion by decompressor at last.Reclaim carbon dioxide purity height, energy-conservation.
Beneficial effect: (1) is compared with the pure amine absorption process that adopts at present extensively, and native system does not adopt the solvent of chemical reaction such as hydramine, has avoided problems such as the corrodibility of the generation of toxic substance and equipment is serious;
(2) it is higher that this system's capture separates the carbon dioxide purity that obtains, and can directly use in some fields, and the capture rate of carbonic acid gas improves, and realizes carbon dioxide zero discharge;
(3) compare with the traditional method that obtains the gaseous carbon dioxide product, the carbonic acid gas after catching is liquid, can directly be pressurized to solution with pump and store, and saves the liquefaction energy consumption;
(4) compare with traditional low temperature method, more only use the collecting carbonic anhydride separation rate of liquefied separation method to improve on the one hand, separate comparatively thorough; More only use the energy consumption of the method for sublimating to decrease on the other hand.
Description of drawings
Fig. 1 is structural representation of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is done further explanation.
As shown in Figure 1, the novel carbon dioxide capture device that a kind of liquefaction is sublimated again, it has comprised the strainer 1, adsorber 2, moisture eliminator 3, first interchanger 4, compressor 5 and second interchanger 6 that connect successively.Unstripped gas makes unstripped gas carry out drying, purification earlier before capturing carbon dioxide gas by strainer 1, adsorber 2 and moisture eliminator 3; Remove some solid impurities by strainer 1, absorb sour gas by adsorber 2 then, remove moisture by moisture eliminator 3 at last.Compare with the pure amine absorption process that adopts at present extensively, native system does not adopt the solvent of chemical reaction such as hydramine, has avoided problems such as the corrodibility of the generation of toxic substance and equipment is serious.
The outlet of second interchanger 6 is connected with No. three unstripped gas entrances of the 3rd interchanger 7, the interface of the 3rd interchanger 7 also comprises No. three unstripped gas outlets, described No. three unstripped gass outlet is connected with the entrance of the 4th interchanger 8, and the outlet of the 4th interchanger 8 is connected with No. five unstripped gas entrances of the 5th interchanger 9; The interface of described the 5th interchanger 9 also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and described No. five unstripped gass outlet is connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower 10 by the condensation pond of pipeline through sublimate knockout tower 11 and No. two knockout towers 12 of sublimating; The refrigeration equipment of knockout tower 11 and the knockout tower 12 of sublimating for No. two of sublimating for No. one is the cascade refrigeration machine, the interface of described gas-liquid separation tower 10 has also comprised the outlet of gas-liquid separation tower carbonic acid gas and has reclaimed assorted residual air body entrance, described gas-liquid separation tower carbonic acid gas outlet is connected with pump 14 entrances, the outlet of a pump 14 is connected with the rectifying tower carbonic acid gas entrance of rectifying tower 15, the interface of described rectifying tower 15 also comprises the outlet of rectifying tower carbon dioxide liquid and rectifying tower tower top outlet, the logical air inlet liquid knockout tower 10 of rectifying tower tower top outlet gas further reclaims separation carbonic acid gas wherein, the outlet of rectifying tower carbonic acid gas is connected with No. five liquid carbon dioxide entrances, No. five liquid carbon dioxide outlets are connected with No. two pump 16 entrances, the outlet of No. two pumps 16 is connected with reservoir 17, because the pressure in the condensation pond is higher than carbonic acid gas triple point force value, make sublimate that separated products dry ice is melted into liquid but not directly distillation be gas, and purity is very high, the carbon dioxide liquid of melting directly is connected with No. five Liquid carbon dioxide entrances by the knockout tower carbonic acid gas outlet of sublimating collects.It is higher that this system's capture separates the carbon dioxide purity that obtains, and can directly use in some fields, and the capture rate of carbonic acid gas improves, and realizes carbon dioxide zero discharge.
The interface of described the 3rd interchanger 7 also comprises No. three nitrogen separation entrances and No. three nitrogen separation gas outlets; The interface of described gas-liquid separation tower 10 also comprises gas-liquid separation tower nitrogen outlet, gas-liquid separation tower nitrogen inlet and gas-liquid knockout tower mixed gas outlet; Wherein, No. three nitrogen separation entrances are connected with gas-liquid separation tower nitrogen outlet; The gas-liquid separation tower mixed gas outlet of described gas-liquid separation tower 10 is connected with the knockout tower gas mixture entrance of sublimating of the knockout tower 11 of sublimating, the interface of the described knockout tower 11 of sublimating also comprises the knockout tower nitrogen inlet of sublimating No. one, the knockout tower nitrogen outlet of sublimating for No. one, the knockout tower carbonic acid gas of sublimating for No. one outlet and the knockout tower mixed gas outlet of sublimating for No., the described knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, the knockout tower nitrogen inlet of sublimating for No. one is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers 12 of sublimating, the knockout tower carbonic acid gas of sublimating for No. one outlet is connected with No. five Liquid carbon dioxide entrances, the interface of described No. two knockout towers 12 of sublimating has also comprised the knockout tower gas mixture entrance of sublimating No. two, the knockout tower mixed gas outlet of sublimating for No. two, the knockout tower carbonic acid gas of sublimating for No. two outlet and the knockout tower nitrogen inlet of sublimating for No. two, the knockout tower mixed gas outlet of wherein sublimating for No. one is connected with No. two knockout tower gas mixture entrances of sublimating, the knockout tower carbonic acid gas of sublimating for No. two outlet is connected with No. five Liquid carbon dioxide entrances, the knockout tower mixed gas outlet of sublimating for No. two is connected with the entrance of decompressor 13, the outlet of decompressor 13 and the knockout tower nitrogen inlet of sublimating for No. two, described decompressor 13 is cryogenic turboexpander.The knockout tower branch two-stage of wherein sublimating, thereby make first step institute chilling requirement temperature drift, reduce the refrigeration requirement of lower temperature position, constant down in identical refrigeration requirement, save the required power consumption of refrigeration, sublimating, institute's chilling requirement part is provided by the backflow cryogen in the knockout tower, and another part is provided by the external refrigeration device.
High carbon dioxide containing gas is example with the oxygen-enriched combusting flue gas, and in conjunction with Fig. 1, this technical process: the carbonic acid gas flue gas of high-content at first removes some solid impurities by strainer 1, removes gas behind the solid impurity and enters adsorber 2 and absorb H
2Sour gas such as S, NOx, SOx enter moisture eliminator 3 afterwards and remove wherein moisture; Suppose through each substances content in the gas mixture after the preliminary treatment and be: nitrogen is 50%, carbonic acid gas is 50%, 0.1MPa, 398.15K.At first be chilled to normal temperature in advance through first interchanger, 4 water-cooleds, its parameter becomes 0.1MPa, 298.15K.Be pressurized to 2MPa through isothermal compression then, behind the cold of outside cooling and utilization backflow nitrogen, enter gas-liquid separation tower 10.By 2MPa carbon dioxide dividing potential drop, determine in the gas-liquid separation tower 10 that carbonic acid gas solid do not occur and can reach concentration, thereby determine that gas-liquid separation tower 10 exit gas concentration of carbon dioxide are 26%.Liquid after the gas-liquid separation enters rectifying tower 15 to carry out rectifying and obtains highly purified Liquid carbon dioxide, and rectifying tower 15 tower top outlet gas backstreamings are further reclaimed and separated to gas-liquid separation tower 10; Gas after the gas-liquid separation enters to sublimate in sublimate for No. one knockout tower 11 and No. two knockout towers 12 of sublimating and separates, carbonic acid gas is sublimated and is solid on the heat exchanger surface in tower, the heat exchangers in towers outside surface is provided with electronic revolving scraper, scrape by electronic revolving scraper afterwards, by the higher relatively temperature of just leading to the unstripped gas of coming in dry ice is melted, the Liquid carbon dioxide that the Liquid carbon dioxide after dry ice melts obtains with rectifying tower 15 is forced into 11MPa by No. two pumps 16 and stores in the reservoir 17.Described sublimate knockout tower 11 and the 12 fens two-stages of knockout tower of sublimating for No. two, thereby make first step institute chilling requirement temperature drift, reduce the refrigeration requirement of lower temperature position, constant down in identical refrigeration requirement, save the required power consumption of extraneous refrigeration, sublimating, institute's chilling requirement part is provided by the backflow cryogen in the knockout tower, and another part is provided by the external refrigeration device; The gas temperature of tower of going out to sublimate is-155.8 ℃, and this moment, gas concentration lwevel was 1ppm, reached higher degree of separation, and this moment, nitrogen gas purity was also higher.The nitrogen pressure of this moment and the cold that carries can utilize again, can reclaim work of expansion on the one hand by the expansion of cryogenic expansion machine, can obtain cold on the one hand.Can make the energy utilization efficiency of total system the highest for the knockout tower 11 of sublimating, sublimate for No. two knockout tower 12, gas-liquid separation tower 10 and a unstripped gas precooling partly provide cold.
The above only is preferred implementation of the present invention; should be pointed out that for those skilled in the art, under the prerequisite that does not break away from the principle of the invention; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (6)
1. novel carbon dioxide capture device that liquefaction is sublimated again is characterized in that: it has comprised the strainer (1), adsorber (2), moisture eliminator (3), first interchanger (4), compressor (5) and second interchanger (6) that connect successively; The outlet of described second interchanger (6) is connected with No. three unstripped gas entrances of the 3rd interchanger (7), the interface of the 3rd interchanger (7) also comprises No. three unstripped gas outlets, described No. three unstripped gass outlet is connected with the entrance of the 4th interchanger (8), and the outlet of the 4th interchanger (8) is connected with No. five unstripped gas entrances of the 5th interchanger (9); The interface of described the 5th interchanger (9) also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and described No. five unstripped gass outlet is connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower (10); The interface of described gas-liquid separation tower (10) has comprised that also the outlet of gas-liquid separation tower carbonic acid gas and rectifying tower (15) overhead gas reclaim entrance, described gas-liquid separation tower carbonic acid gas outlet is connected with a pump (14) entrance, the outlet of a pump (14) is connected with the rectifying tower carbonic acid gas entrance of rectifying tower (15), the interface of described rectifying tower (15) also comprises the outlet of rectifying tower carbonic acid gas and the outlet of rectifying tower overhead gas, the outlet of rectifying tower overhead gas is connected with the gas recovery entrance of gas-liquid separation tower (10), the outlet of rectifying tower carbonic acid gas is connected with No. five liquid carbon dioxide entrances, No. five liquid carbon dioxide outlets are connected with No. two pumps (16) entrance, and the outlet of No. two pumps (16) is connected with reservoir (17).
2. a kind of liquefaction according to claim 1 novel carbon dioxide capture device of sublimating again, it is characterized in that: the interface of described the 3rd interchanger (7) comprises No. three nitrogen separation entrances and No. three nitrogen separation gas outlets; The interface of described gas-liquid separation tower (10) also comprises gas-liquid separation tower nitrogen outlet, gas-liquid separation tower nitrogen inlet and gas-liquid knockout tower mixed gas outlet; Wherein, No. three nitrogen separation entrances are connected with gas-liquid separation tower nitrogen outlet; The gas-liquid separation tower mixed gas outlet of described gas-liquid separation tower (10) is connected with the knockout tower gas mixture entrance of sublimating of the knockout tower of sublimating (11), the interface of the described knockout tower of sublimating (11) also comprises the knockout tower nitrogen inlet of sublimating No. one, the knockout tower nitrogen outlet of sublimating for No. one, the knockout tower carbonic acid gas of sublimating for No. one outlet and the knockout tower mixed gas outlet of sublimating for No., the described knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, the knockout tower nitrogen inlet of sublimating for No. one is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers of sublimating (12), and the knockout tower carbonic acid gas outlet of sublimating is connected with No. five Liquid carbon dioxide entrances; The interface of described No. two knockout towers of sublimating (12) has also comprised the knockout tower gas mixture entrance of sublimating No. two, the knockout tower mixed gas outlet of sublimating for No. two, the knockout tower carbonic acid gas of sublimating for No. two outlet and the knockout tower nitrogen inlet of sublimating for No. two, the knockout tower mixed gas outlet of wherein sublimating for No. one is connected with No. two knockout tower gas mixture entrances of sublimating, the knockout tower carbonic acid gas of sublimating for No. two outlet is connected with No. five Liquid carbon dioxide entrances, the knockout tower mixed gas outlet of sublimating for No. two is connected with the entrance of decompressor (13), and the outlet of decompressor (13) is connected with No. two knockout tower nitrogen inlets of sublimating.
3. a kind of liquefaction according to claim 1 novel carbon dioxide capture device of sublimating again, it is characterized in that: described No. five unstripped gass outlet is connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower (10) by the condensation pond of pipeline through the knockout tower of sublimating (11) and No. two knockout towers of sublimating (12).
4. a kind of liquefaction according to claim 1 novel carbon dioxide capture device of sublimating again, it is characterized in that: described decompressor (13) is cryogenic turboexpander.
5. a kind of liquefaction according to claim 1 novel carbon dioxide capture device of sublimating again, it is characterized in that: the refrigeration equipment of the knockout tower of sublimating (11) and No. two knockout towers of sublimating (12) is the cascade refrigeration machine.
6. a kind of liquefaction according to claim 1 novel carbon dioxide capture device of sublimating again, it is characterized in that: the inner heat exchanger surface of the knockout tower of sublimating (11) and No. two knockout towers of sublimating (12) is respectively equipped with electronic revolving scraper.
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Cited By (9)
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| CN104998513A (en) * | 2015-07-21 | 2015-10-28 | 苏州市兴鲁空分设备科技发展有限公司 | Carbon dioxide rectification emission-reducing process and apparatus thereof |
| CN107792854A (en) * | 2016-08-30 | 2018-03-13 | 中国石油集团钻井工程技术研究院 | High concentration liquid carbon dioxide trapping system and method |
| CN110986637A (en) * | 2019-12-06 | 2020-04-10 | 山东神舟制冷设备有限公司 | CO2Prying block for U-shaped gas separation heat exchanger |
| CN112516614A (en) * | 2020-11-17 | 2021-03-19 | 天津大学合肥创新发展研究院 | Power device flue gas carbon dioxide emission reduction system |
| CN113175687A (en) * | 2021-05-28 | 2021-07-27 | 哈尔滨工业大学 | Flue gas carbon dioxide capturing and purifying system and method |
| WO2021196423A1 (en) * | 2020-04-01 | 2021-10-07 | 厦门理工学院 | Circulating solid co2 cleaning system |
| CN114682042A (en) * | 2022-02-22 | 2022-07-01 | 江苏科技大学 | Ship tail gas treatment system and treatment method thereof |
| CN115025512A (en) * | 2022-05-23 | 2022-09-09 | 浙江大学 | Switching type CO 2 Desublimation separation system |
| CN115385374A (en) * | 2022-08-26 | 2022-11-25 | 神华准能资源综合开发有限公司 | Preparation device and preparation method of gallium trichloride |
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2013
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104998513A (en) * | 2015-07-21 | 2015-10-28 | 苏州市兴鲁空分设备科技发展有限公司 | Carbon dioxide rectification emission-reducing process and apparatus thereof |
| CN104998513B (en) * | 2015-07-21 | 2017-07-21 | 苏州市兴鲁空分设备科技发展有限公司 | Carbon dioxide rectifying emission-reducing process and device |
| CN107792854A (en) * | 2016-08-30 | 2018-03-13 | 中国石油集团钻井工程技术研究院 | High concentration liquid carbon dioxide trapping system and method |
| CN110986637A (en) * | 2019-12-06 | 2020-04-10 | 山东神舟制冷设备有限公司 | CO2Prying block for U-shaped gas separation heat exchanger |
| WO2021196423A1 (en) * | 2020-04-01 | 2021-10-07 | 厦门理工学院 | Circulating solid co2 cleaning system |
| CN112516614A (en) * | 2020-11-17 | 2021-03-19 | 天津大学合肥创新发展研究院 | Power device flue gas carbon dioxide emission reduction system |
| CN113175687A (en) * | 2021-05-28 | 2021-07-27 | 哈尔滨工业大学 | Flue gas carbon dioxide capturing and purifying system and method |
| CN113175687B (en) * | 2021-05-28 | 2024-07-23 | 哈尔滨工业大学 | System and method for capturing and purifying carbon dioxide in flue gas |
| CN114682042A (en) * | 2022-02-22 | 2022-07-01 | 江苏科技大学 | Ship tail gas treatment system and treatment method thereof |
| CN114682042B (en) * | 2022-02-22 | 2022-12-27 | 江苏科技大学 | Ship tail gas treatment system and treatment method thereof |
| CN115025512A (en) * | 2022-05-23 | 2022-09-09 | 浙江大学 | Switching type CO 2 Desublimation separation system |
| CN115385374A (en) * | 2022-08-26 | 2022-11-25 | 神华准能资源综合开发有限公司 | Preparation device and preparation method of gallium trichloride |
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| Publication number | Publication date |
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| CN103274406B (en) | 2015-02-11 |
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