CN103274406B - Novel carbon dioxide trapping device performing liquefaction and sublimation - Google Patents
Novel carbon dioxide trapping device performing liquefaction and sublimation Download PDFInfo
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- CN103274406B CN103274406B CN201310234666.9A CN201310234666A CN103274406B CN 103274406 B CN103274406 B CN 103274406B CN 201310234666 A CN201310234666 A CN 201310234666A CN 103274406 B CN103274406 B CN 103274406B
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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
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- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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
Carbonated for richness unstripped gas by isolating carbonic acid gas for compression, the type of cooling, is belonged to refrigeration and cryogenic technology field by the present invention.
Background technology
While industrial development process fast brings convenient life, also bring huge environmental problem, according to USDOE statistics, the carbonic acid gas discharged because of combustion of fossil fuels every year reaches more than 30,000,000,000 tons, but also in continuous growth.The heavy industry such as power station, oil factory, Steel Plant of combustion of fossil fuels is the main source of Carbon emission, the carbon dioxide in flue gas volume content of power plant emission is about about 15%, comparatively power plant is high for the carbon dioxide in flue gas volume content of some Metallurgical Factories discharge, is about about 35%.Contain except great amount of carbon dioxide except in the flue gas that power plant, metallurgy industry burning mineral fuel produce, also a certain amount of carbonic acid gas is contained in undressed biogas and Sweet natural gas, in gas material, carbon dioxide content is between 5% to 98%, thus has an impact to the quality of biogas and Sweet natural gas.
On the other hand, carbonic acid gas is a kind of very valuable resource, has higher civilian and industrial value, has now been widely used in the departments such as foodstuffs industry, chemical industry, mechanical industry, agricultural, business, transport, oil production, national defence, fire-fighting.Mainly comprise physics to utilize and chemical utilization: the Main physical purposes of carbonic acid gas comprises for the manufacture of the extraction agent of the additive of dry ice, supercritical extraction solvent, beverage and beer, fire-fighting medium, spices and medicine, clean-out system, for tobacco expanding, replaces Chlorofluorocarbons (CFCs) to be used as whipping agent, gaseous fertilizer and for enhanced oil recovery (EOR) etc.; Its Chemical activator is mainly that raw material can produce multiple organic and inorganic chemical product with carbonic acid gas, in chemical industry, utilizes the mainly urea of carbonic acid gas, soda ash and bicarbonate of ammonia on a large scale.
For the control problem of Carbon emission, domestic and international insider has carried out long felt, and to control the most direct effective means that carbonic acid gas increases in a short time be the trapping 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.Solution absorption method technology maturation, apply comparatively extensive, but this method causes energy consumption larger because regeneration stage needs amount of heat, prepare absorption agent and need a large amount of energy consumption and absorption agent has corrodibility and toxicity, simultaneously stability agent can be lost efficacy in the process of repeatedly carrying out absorption and regeneration, needs constantly to supplement; Pressure swing adsorption process non-corrosiveness medium, running maintenance expense are low, but for obtaining higher carbon dioxide purity, need comparatively multiple adsorption tower, equipment control is comparatively difficult, invests higher; Membrane separation process technological process is simple, easy to operate, but its to unstripped gas require little compared with its treatment capacity of high, present stage, filming technology is complicated, membrane stability is poor., also there is common problem in above common method, is namely separated the CO 2 obtained and is gas, requires the expenditure of energy and be processed into liquid further so that transport is sealed up for safekeeping.In addition, the CO 2 purity of institute's separating trap is generally difficult to reach direct applied specification, if to need the Carbon Dioxide Application after catching in each industry, then to need further purification.
Summary of the invention
Goal of the invention: the object of the invention is to overcome the deficiencies in the prior art, propose the Novel carbon dioxide trap setting that a kind of liquefaction is sublimated again, this device is separated mainly for the collecting carbonic anhydride in the carbonated gas mixture of height, improves the trapping purity of carbonic acid gas, increases the capture rate of 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 trap setting that liquefaction is sublimated again, it includes the strainer, adsorber, moisture eliminator, First Heat Exchanger, compressor and the second interchanger that connect successively, the outlet of the second described 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, No. three described unstripped gas outlets are 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 the 5th described interchanger also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and No. five described unstripped gas outlets are connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower, the interface of described gas-liquid separation tower further comprises gas-liquid separation tower carbon dioxide outlet and gas recovery entrance, described gas-liquid separation tower carbon dioxide outlet is connected with a pump intake, a pump outlet is connected with the rectifying tower carbonic acid gas entrance of rectifying tower, the interface of described rectifying tower also comprises rectifying tower carbon dioxide outlet and the outlet of rectifying tower top gaseous body, the outlet of rectifying tower top gaseous body is reclaimed entrance with gas-liquid separation tower and is connected, rectifying tower carbon dioxide outlet is connected with No. five liquid carbon dioxide entrances, No. five liquid carbon dioxide outlets are connected with No. two pump intakes, No. two pump outlet are connected with reservoir.
Wherein, the interface of the 3rd described 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 separation 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 No. one of a knockout tower of sublimating knockout tower gas mixture entrance of sublimating, the interface of a described knockout tower of sublimating also comprises a knockout tower nitrogen inlet of sublimating, a knockout tower nitrogen outlet of sublimating, sublimate knockout tower carbon dioxide outlet and a knockout tower mixed gas outlet of sublimating, described No. one knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, a knockout tower nitrogen inlet of sublimating is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers of sublimating, a knockout tower carbon dioxide outlet of sublimating is connected with No. five Liquid carbon dioxide entrances, the interface of No. two described knockout towers of sublimating further comprises No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower mixed gas outlets of sublimating, No. two sublimate knockout tower carbon dioxide outlet and No. two knockout tower nitrogen inlets of sublimating, wherein a knockout tower mixed gas outlet of sublimating is connected with No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower carbon dioxide outlet of sublimating are connected with No. five Liquid carbon dioxide entrances, No. two knockout tower mixed gas outlets of sublimating are connected with the entrance of decompressor, the outlet of decompressor is connected with No. two knockout tower nitrogen inlets of sublimating.
Wherein, No. five described unstripped gas outlets are connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower with the condensation pond of No. two knockout towers of sublimating through a knockout tower of sublimating by pipeline.
Wherein, described decompressor is cryogenic turboexpander.
Wherein, the refrigeration equipment of described sublimate knockout tower and No. two knockout towers of sublimating is cascade refrigeration machine.
Wherein, the heat exchanger surface of sublimate knockout tower and No. two knockout tower inside of sublimating is respectively equipped with electronic rotation scraper.
Unstripped gas first successively by strainer, adsorber and moisture eliminator, makes unstripped gas just first carry out drying, purification before capturing carbon dioxide gas by the present invention.Native system does not adopt the solvent of the chemical reactions such as hydramine, avoids the 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 gas-liquid separation tower, can directly lay in, continuation cooling is afterwards sublimated and is isolated dry ice.Gas after being separated with No. two knockout towers of sublimating by a knockout tower of sublimating, the content wherein containing carbonic acid gas is lower, guarantees not produce dry ice damage equipment, reclaims cold and work of expansion finally by decompressor.Reclaim carbon dioxide purity high, energy-conservation.
Beneficial effect: (1), compared with the alcohol amine absorption process adopted at present extensively, native system does not adopt the solvent of the chemical reactions such as hydramine, avoids the problems such as the corrodibility of the generation of toxic substance and equipment is serious;
(2) to be separated the carbon dioxide purity that obtains higher for the trapping of this system, and can directly apply in some fields, the capture rate of carbonic acid gas improves, and realizes carbon dioxide zero discharge;
(3) compared with obtaining the traditional method of gaseous carbon dioxide product, the carbonic acid gas after catching is liquid, can be pressurized to solution storage by direct pump, saves liquefaction energy consumption;
(4) compared with Conventional cryogenic method, more only use the collecting carbonic anhydride separation rate of liquefied separation method to improve on the one hand, be separated comparatively thorough; The energy consumption of method of sublimating more only is used to decrease on the other hand.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention done and further explain.
As shown in Figure 1, the Novel carbon dioxide trap setting that a kind of liquefaction is sublimated again, it includes the strainer 1, adsorber 2, moisture eliminator 3, First Heat Exchanger 4, compressor 5 and the second interchanger 6 that connect successively.Unstripped gas, by strainer 1, adsorber 2 and moisture eliminator 3, makes unstripped gas first carry out drying, purification before capturing carbon dioxide gas; Remove some solid impurities by strainer 1, then absorb sour gas by adsorber 2, remove moisture finally by moisture eliminator 3.Compared with the alcohol amine absorption process adopted at present extensively, native system does not adopt the solvent of the chemical reactions such as hydramine, avoids the problems such as the corrodibility of the generation of toxic substance and equipment is serious.
The outlet of the 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, No. three described unstripped gas outlets are 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 the 5th described interchanger 9 also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and No. five described unstripped gas outlets are connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower 10 with the condensation pond of No. two knockout towers 12 of sublimating through a knockout tower 11 of sublimating by pipeline, the refrigeration equipment of sublimate knockout tower 11 and No. two knockout towers 12 of sublimating is cascade refrigeration machine, the interface of described gas-liquid separation tower 10 further comprises gas-liquid separation tower carbon dioxide outlet and reclaims assorted remaining gas inlet, described gas-liquid separation tower carbon dioxide outlet is connected with 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 carbon dioxide liquid and rectifying tower tower top outlet, rectifying tower ejects gas and leads to and carry out further reclaiming the carbonic acid gas be separated wherein into gas-liquid separation tower 10, rectifying tower carbon dioxide outlet 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 condensation pond is higher than carbonic acid gas triple point pressure value, the isolated product dry ice that makes to sublimate is melted into liquid and non-immediate distillation is gas, and purity is very high, the carbon dioxide liquid of thawing is directly connected with No. five Liquid carbon dioxide entrances by knockout tower carbon dioxide outlet of sublimating and collects.It is higher that the trapping of this system is separated the carbon dioxide purity obtained, and can directly apply in some fields, and the capture rate of carbonic acid gas improves, and realizes carbon dioxide zero discharge.
The interface of the 3rd described 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 separation 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 No. one of a knockout tower 11 of sublimating knockout tower gas mixture entrance of sublimating, the interface of described No. one knockout tower 11 of sublimating also comprises a knockout tower nitrogen inlet of sublimating, a knockout tower nitrogen outlet of sublimating, sublimate knockout tower carbon dioxide outlet and a knockout tower mixed gas outlet of sublimating, described No. one knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, a knockout tower nitrogen inlet of sublimating is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers 12 of sublimating, a knockout tower carbon dioxide outlet of sublimating is connected with No. five Liquid carbon dioxide entrances, the interface of described No. two knockout towers 12 of sublimating further comprises No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower mixed gas outlets of sublimating, No. two sublimate knockout tower carbon dioxide outlet and No. two knockout tower nitrogen inlets of sublimating, wherein a knockout tower mixed gas outlet of sublimating is connected with No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower carbon dioxide outlet of sublimating are connected with No. five Liquid carbon dioxide entrances, No. two knockout tower mixed gas outlets of sublimating are connected with the entrance of decompressor 13, the outlet of decompressor 13 and No. two knockout tower nitrogen inlets of sublimating, described decompressor 13 is cryogenic turboexpander.Wherein to sublimate knockout tower point two-stage, thus make first step institute chilling requirement temperature drift, reduce the refrigeration requirement compared with low-temperature level, under identical refrigeration requirement is constant, save the required power consumption of refrigeration, institute's chilling requirement part in knockout tower of sublimating is provided by refluxed cryogenic fluid, and another part is provided by external refrigeration device.
High carbon dioxide containing gas is for oxygen-enriched combusting flue gas, and composition graphs 1, this technical process: first the carbonic acid gas flue gas of high-content removes some solid impurities by strainer 1, removes the gas after solid impurity and enter adsorber 2 and absorb H
2the sour gas such as S, NOx, SOx, enter moisture eliminator 3 afterwards and remove moisture wherein; Assuming that each substances content is in gas mixture after preliminary treatment: nitrogen is 50%, carbonic acid gas is 50%, 0.1MPa, 398.15K.First be chilled to normal temperature in advance through First Heat Exchanger 4 water-cooled, its parameter becomes 0.1MPa, 298.15K.Then be pressurized to 2MPa through isothermal compression, through outside cooling and utilization backflow nitrogen cold after, enter gas-liquid separation tower 10.By 2MPa carbon dioxide dividing potential drop, determine that in gas-liquid separation tower 10, carbonic acid gas does not occur that solid can reach concentration, thus the concentration determining gas-liquid separation tower 10 exit gas carbonic acid gas is 26%.Liquid after gas-liquid separation enters rectifying tower 15 to carry out rectifying and obtains highly purified Liquid carbon dioxide, and the gas backstreaming of rectifying tower 15 tower top outlet, to gas-liquid separation tower 10, reclaims separation further; Gas after gas-liquid separation enters a knockout tower 11 of sublimating to carry out sublimating being separated with in No. two knockout towers 12 of sublimating, on heat exchanger surface in tower, carbonic acid gas is sublimated as solid, heat exchangers in towers outside surface is provided with electronic rotation scraper, scraped by electronic rotation scraper afterwards, by the relatively high temperature of just leading to the unstripped gas of coming in, dry ice is melted, be forced into 11MPa by No. two pumps 16 together with the Liquid carbon dioxide that the Liquid carbon dioxide after dry ice melts and rectifying tower 15 obtain and be stored in reservoir 17.Described No. one sublimate knockout tower 11 and No. two knockout tower 12 points of two-stages of sublimating, thus make first step institute chilling requirement temperature drift, reduce the refrigeration requirement compared with low-temperature level, under identical refrigeration requirement is constant, save the required power consumption of extraneous refrigeration, institute's chilling requirement part in knockout tower of sublimating is provided by refluxed cryogenic fluid, and another part is provided by external refrigeration device; The gas temperature of tower of going out to sublimate is-155.8 DEG C, and now gas concentration lwevel is 1ppm, and reach higher degree of separation, now nitrogen gas purity is also higher.Nitrogen pressure now and the cold carried can utilize again, by the expansion of cryogenic expansion machine, reclaim work of expansion on the one hand, can obtain cold on the one hand.Cold can be provided for sublimate knockout tower 11, No. two knockout towers 12 of sublimating, gas-liquid separation tower 10 and unstripped gas pre-cooling section, make the energy utilization efficiency of whole system the highest.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles 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 (5)
1. liquefy a Novel carbon dioxide trap setting of sublimating again, it is characterized in that: it includes the strainer (1), adsorber (2), moisture eliminator (3), First Heat Exchanger (4), compressor (5) and the second interchanger (6) that connect successively, the outlet of described the 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, No. three described unstripped gas outlets are 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 the 5th described interchanger (9) also comprises No. five Liquid carbon dioxide entrances, No. five Liquid carbon dioxide outlets and No. five unstripped gas outlets, and No. five described unstripped gas outlets are 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) further comprises gas-liquid separation tower carbon dioxide outlet and rectifying tower (15) overhead gas reclaims entrance, described gas-liquid separation tower carbon dioxide outlet is connected with 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 rectifying tower carbon dioxide outlet and the outlet of rectifying tower top gaseous body, the outlet of rectifying tower top gaseous body is connected with the gas recovery entrance of gas-liquid separation tower (10), rectifying tower carbon dioxide outlet 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),
The interface of the 3rd described 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 separation 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 No. one of a knockout tower of sublimating (11) knockout tower gas mixture entrance of sublimating, the interface of a described knockout tower of sublimating (11) also comprises a knockout tower nitrogen inlet of sublimating, a knockout tower nitrogen outlet of sublimating, sublimate knockout tower carbon dioxide outlet and a knockout tower mixed gas outlet of sublimating, described No. one knockout tower nitrogen outlet of sublimating is connected with gas-liquid separation tower nitrogen inlet, a knockout tower nitrogen inlet of sublimating is connected with No. two tower nitrogen outlets of sublimating of No. two knockout towers of sublimating (12), a knockout tower carbon dioxide outlet of sublimating is connected with No. five Liquid carbon dioxide entrances, the interface of No. two described knockout towers of sublimating (12) further comprises No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower mixed gas outlets of sublimating, No. two sublimate knockout tower carbon dioxide outlet and No. two knockout tower nitrogen inlets of sublimating, wherein a knockout tower mixed gas outlet of sublimating is connected with No. two knockout tower gas mixture entrances of sublimating, No. two knockout tower carbon dioxide outlet of sublimating are connected with No. five Liquid carbon dioxide entrances, No. two knockout tower mixed gas outlets of sublimating are connected with the entrance of decompressor (13), the outlet of decompressor (13) is connected with No. two knockout tower nitrogen inlets of sublimating.
2. a kind of liquefaction according to claim 1 Novel carbon dioxide trap setting of sublimating again, is characterized in that: No. five described unstripped gass outlets are connected with the gas-liquid separation tower unstripped gas entrance of gas-liquid separation tower (10) with the condensation pond of No. two knockout towers of sublimating (12) through a knockout tower of sublimating (11) by pipeline.
3. a kind of liquefaction according to claim 1 Novel carbon dioxide trap setting of sublimating again, is characterized in that: described decompressor (13) is cryogenic turboexpander.
4. a kind of liquefaction according to claim 1 Novel carbon dioxide trap setting of sublimating again, is characterized in that: the refrigeration equipment of a knockout tower of sublimating (11) and No. two knockout towers of sublimating (12) is cascade refrigeration machine.
5. a kind of liquefaction according to claim 1 Novel carbon dioxide trap setting of sublimating again, is characterized in that: a knockout tower of sublimating (11) and the inner heat exchanger surface of No. two knockout towers of sublimating (12) are respectively equipped with electronic rotation scraper.
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| 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 |
| CN110986637B (en) * | 2019-12-06 | 2020-12-08 | 山东神舟制冷设备有限公司 | CO2Prying block for U-shaped gas separation heat exchanger |
| CN111530848A (en) * | 2020-04-01 | 2020-08-14 | 厦门理工学院 | Circulating solid CO2Cleaning 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 |
| CN114682042B (en) * | 2022-02-22 | 2022-12-27 | 江苏科技大学 | Ship tail gas treatment system and treatment method thereof |
| CN115025512B (en) * | 2022-05-23 | 2023-07-07 | 浙江大学 | Switching type CO 2 De-sublimating 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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