CN217449626U - Device for continuously capturing and separating carbon dioxide in flue gas by single stage through hydrate method - Google Patents
Device for continuously capturing and separating carbon dioxide in flue gas by single stage through hydrate method Download PDFInfo
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- CN217449626U CN217449626U CN202221233066.1U CN202221233066U CN217449626U CN 217449626 U CN217449626 U CN 217449626U CN 202221233066 U CN202221233066 U CN 202221233066U CN 217449626 U CN217449626 U CN 217449626U
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 134
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 67
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 67
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 239000003546 flue gas Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000007789 gas Substances 0.000 claims abstract description 114
- 238000006703 hydration reaction Methods 0.000 claims abstract description 58
- 239000007788 liquid Substances 0.000 claims abstract description 50
- 230000036571 hydration Effects 0.000 claims abstract description 48
- 230000007246 mechanism Effects 0.000 claims abstract description 18
- 238000003756 stirring Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims description 24
- 238000002156 mixing Methods 0.000 claims description 20
- 238000003860 storage Methods 0.000 claims description 19
- 238000001514 detection method Methods 0.000 claims description 12
- 238000005070 sampling Methods 0.000 claims description 10
- 238000004817 gas chromatography Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000010907 mechanical stirring Methods 0.000 claims description 3
- 230000008878 coupling Effects 0.000 claims description 2
- 238000010168 coupling process Methods 0.000 claims description 2
- 238000005859 coupling reaction Methods 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 239000003595 mist Substances 0.000 abstract description 3
- 238000000354 decomposition reaction Methods 0.000 abstract description 2
- 239000002912 waste gas Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- 239000000243 solution Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical group OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 150000004677 hydrates Chemical class 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910052599 brucite Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 description 1
- 239000002041 carbon nanotube Substances 0.000 description 1
- 229910021393 carbon nanotube Inorganic materials 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 229910021389 graphene Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model relates to a device for continuously capturing and separating carbon dioxide in flue gas by a single stage of a hydrate method, which comprises a gas supply system, a balance kettle, a hydration tower, a gas collecting tank and a jacket type high-low temperature circulating condenser; a stirring mechanism is arranged in the hydration tower, the upper part of the hydration tower is provided with an air inlet pipe, a first exhaust pipe, a second exhaust pipe and a liquid inlet pipe, and the bottom of the hydration tower is provided with a liquid discharge pipe; the balance kettle is connected with the air inlet pipe, and a first valve is arranged on the air inlet pipe; the first exhaust pipe is provided with a second valve, the second exhaust pipe is connected with the gas collection tank, and the second exhaust pipe is provided with a third valve; the liquid inlet pipe is provided with a fourth valve, and the liquid outlet pipe is provided with a fifth valve. The utility model discloses in, the mist flows through single-stage hydration tower and separates in succession, and promoter solution flows through feed liquor pump recycle, and the formation and the decomposition of hydrate all go on under more mild condition, and equipment cost, running cost are lower, can not produce waste gas waste water etc. accord with the environmental protection requirement.
Description
Technical Field
The utility model belongs to carbon dioxide entrapment field, especially a device that is arranged in continuous entrapment of hydrate method single-stage to separate carbon dioxide in the flue gas.
Background
Carbon dioxide (CO) 2 ) As one of the main components of greenhouse gases, it accounts for about 63% of the total amount of greenhouse gases. With the improvement of the environmental protection requirement, the emission reduction of carbon dioxide is urgent. Carbon dioxide capture is one of the important ways to realize carbon neutralization as a key link of carbon dioxide capture utilization and sequestration technology (CCUS).
Currently, there are several specific carbon dioxide separation technologies in the traditional industry, and the most common are the following four technologies: absorption, adsorption, cryogenic separation, membrane separation. The adsorption method needs to pressurize the gas in advance, and the temperature needs to be raised during desorption, so that the energy consumption is high. In addition, the traditional method utilizes a method for sealing and storing carbon dioxide in flue gas by brucite, has higher efficiency and lower energy consumption, but CO 2 The sealing technique is too costly and results in wasted resources, which may have negative environmental impact if not handled properly. Therefore, the development of a carbon dioxide recycling device with low energy consumption, large gas storage capacity, safety, stability, low investment, environmental protection and no pollution is urgently needed.
CO capture with hydrate formation 2 The hydrate is an emerging technology, and is a non-stoichiometric enveloping compound with the shape similar to ice, which is formed by a plurality of small molecule gases and water under the conditions of high pressure and low temperature. Gas hydrates are selective to gas during their formation, and differ from each otherThe gas has different temperature and pressure when generating the hydrate, and the gas which is easy to generate the hydrate is enriched in the hydrate phase by controlling the temperature and pressure change in the process of generating the hydrate, thereby achieving the purpose of separation. Compared with the traditional separation method, the principle and the process of the hydrate separation method are simpler, the process flow is green and pollution-free, the method is insensitive to the impurities in the raw material gas, and the method has low energy consumption and low cost. The reaction conditions required in the separation process of the hydrate method are relatively mild, the pressure and the temperature are easy to realize in the chemical reaction process, and the energy consumption is easy to control. The hydrate method separation process can not generate secondary pollution, and the hydrate generation and separation process only needs gas and water, and can not generate waste and material loss like the traditional separation process.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a device for carbon dioxide in hydrate method single-stage entrapment separation flue gas is provided, and the mist passes through gas circuit circulation continuous separation, and the promoter passes through liquid circuit circulation recycle, can realize generating hydrate, reduce cost under mild condition, and does not produce new gaseous pollutants or liquid.
In order to solve the above problem, the utility model adopts the technical scheme that: the device for capturing and separating the carbon dioxide in the flue gas by the single stage of the hydrate method comprises a gas supply system, a balance kettle, a hydration tower, a gas collecting tank and a jacketed high-low temperature circulating condenser for cooling or heating the hydration tower;
a stirring mechanism is arranged in the hydration tower, an air inlet pipe, a first exhaust pipe, a second exhaust pipe and a liquid inlet pipe are arranged at the upper part of the hydration tower, and a liquid discharge pipe is arranged at the bottom of the hydration tower; the balance kettle is connected with the air inlet pipe, and a first valve is arranged on the air inlet pipe; the first exhaust pipe is provided with a second valve, the second exhaust pipe is connected with the gas collection tank, and the second exhaust pipe is provided with a third valve; and a fourth valve is arranged on the liquid inlet pipe, and a fifth valve is arranged on the liquid discharge pipe.
Further, the fluid-discharge tube is connected with a liquid storage tank, the liquid inlet pipe is communicated with the liquid storage tank, a liquid inlet pump is arranged on the liquid inlet pipe, an accelerant is stored in the liquid storage tank, and the accelerant is recycled through a liquid path.
Furthermore, the gas collecting tank is connected with a gas chromatography detector through a detection pipe, a sixth valve is arranged on the detection pipe, an automatic sampling valve is arranged between the detection pipe and the gas chromatography detector, and CO in the flue gas can be automatically analyzed on line 2 The separation efficiency.
Further, the second exhaust pipe is connected with a vacuum pump.
Further, the gas supply system comprises a plurality of gas storage mechanisms, a condenser and a mixing tank, wherein the plurality of gas storage mechanisms are all connected with the condenser, the condenser is connected with the mixing tank through a pipeline, the mixing tank is connected with a pressure pump through a pipeline, and the pressure pump is connected with the balance kettle through a pipeline; be provided with the seventh valve on the pipeline between condenser and the blending tank, the blending tank with be provided with the eighth valve on the pipeline between the force (forcing) pump, be provided with the ninth valve on the pipeline between force (forcing) pump and the equilibrium cauldron, the mist passes through the gas circuit circulation through single-stage hydration tower single-stage continuous separation.
Further, the gas storage mechanism includes first gas cylinder and second gas cylinder, first gas cylinder with the second gas cylinder all through the pipeline with the condenser links to each other, just first gas cylinder with set gradually tenth valve, first relief pressure valve and first gas flowmeter on the pipeline between the condenser, the second gas cylinder with set gradually eleventh valve, second relief pressure valve and second gas flowmeter on the pipeline between the condenser.
Furthermore, the gas collecting tank is connected with the pressure pump through a circulating pipe, and a twelfth valve is arranged on the circulating pipe.
Further, the stirring mechanism is a magnetic coupling mechanical stirring paddle.
The utility model has the advantages that: the temperature and the pressure of a hydration tower are controlled, an environment suitable for generating a carbon dioxide hydrate is created, carbon dioxide in smoke can be subjected to hydration reaction to generate the hydrate, the carbon dioxide in the smoke is separated, then a second valve on a first exhaust pipe is opened, other gases in the smoke are discharged through the first exhaust pipe, the second valve is closed after the other gases are discharged, the hydrate is heated and heated, the hydrate is decomposed and becomes gaseous carbon dioxide again, a third valve is arranged on a second exhaust pipe, the gaseous carbon dioxide is conveyed to a gas collecting tank through the second exhaust pipe to be stored, the separated carbon dioxide further flows through the hydration tower again through gas circuit circulation to be continuously separated, and the concentration of the carbon dioxide is improved. In the process, the generation and decomposition of the hydrate are carried out under a mild condition, the equipment cost and the operation cost are low, no waste gas and waste water are generated, and the environment-friendly requirement is met.
Drawings
Fig. 1 is an overall schematic view of the present invention;
reference numerals are as follows: 1-a first gas cylinder; 2-a second gas cylinder; 3-tenth valve; 4-an eleventh valve; 5-a first pressure reducing valve; 6-second pressure reducing valve; 7-a first gas flow meter; 8-a second gas flow meter; 9-a condenser; 10-a seventh valve; 11-mixing tank; 12-eighth valve; 13-a pressure pump; 14-a ninth valve; 15-a balance kettle; 16 — a first valve; 17 — a second valve; 18-a hydration tower; 181-stirring mechanism; 182-an air inlet pipe; 183 — first exhaust pipe; 184-second exhaust pipe; 185-liquid inlet pipe; 186-drain pipe; 19-a third valve; 20-a twelfth valve; 21-a gas collecting tank; 22-sixth valve; 23-a vacuum pump; 24-a gas chromatography detector; 25-a liquid storage tank; 26-a fourth valve; 27-a fifth valve; 29-liquid inlet pump; 30-a detection tube; 31-circulation pipe.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
The utility model discloses a device for carbon dioxide in hydrate method single-stage entrapment separation flue gas, as shown in figure 1, including gas supply system, reation kettle 15, hydration tower 18, gas collecting tank 21 and be arranged in cooling down or the high low temperature circulating condenser of double-layered formula that heaies up hydration tower 18. Wherein the gas supply system is used for providing flue gas of carbon dioxide to be separated, and the equilibrium reactor 15 is used for storing the flue gas, so that the flue gas can be fed into the hydration tower 18 in batches. Hydration tower 18 is used for separating carbon dioxide through hydration, and the tower body and the tower at upper and lower both ends change all to adopt 316L stainless steel, and concrete structure is:
the hydration tower 18 is internally provided with a stirring mechanism 181, and the stirring mechanism 181 is used for stirring the materials, so that the carbon dioxide in the flue gas can be fully and uniformly mixed with the liquid, and the carbon dioxide is ensured to be thoroughly separated and extracted. The stirring mechanism 181 may be any conventional stirrer, preferably a magnetically coupled mechanical stirring paddle, and is controlled to rotate at a speed of 00 to 800 rpm. The jacketed high-low temperature circulating condenser is arranged on the outer wall of the hydration tower 18 and used for controlling the temperature in the hydration tower 18, and the medium and the hydration tower 18 exchange heat through introducing media with different temperatures, so that the temperature of the hydration tower 18 is increased or decreased.
An air inlet pipe 182, a first exhaust pipe 183, a second exhaust pipe 184 and a liquid inlet pipe 185 are arranged at the upper part of the hydration tower 18, and a liquid outlet pipe 186 is arranged at the bottom of the hydration tower 18. The balance kettle 15 is connected with the gas inlet pipe 182, and the gas inlet pipe 182 is provided with a first valve 16, so that the flue gas in the balance kettle 15 can enter the hydration tower 18 through the gas inlet pipe 182. The first exhaust pipe 183 is for exhausting gas that is not subjected to the hydration reaction after the hydration reaction, and the second valve 17 is provided in the first exhaust pipe 183. The second exhaust pipe 184 is used for exhausting carbon dioxide separated and extracted from the flue gas, a third valve 19 is arranged on the second exhaust pipe 184, the second exhaust pipe 184 is connected with the gas collecting tank 21, and the gas collecting tank 21 is used for storing carbon dioxide gas. The liquid inlet pipe 185 is used for inputting liquid participating in the hydration reaction, the liquid outlet pipe 186 is used for discharging the liquid participating in the hydration reaction, the fourth valve 26 is arranged on the liquid inlet pipe 185, and the fifth valve 27 is arranged on the liquid outlet pipe 186. The first valve 16, the second valve 17, the third valve 19, the fourth valve 26 and the like are used for controlling the on-off of the pipeline, and ball valves are adopted.
The working process of the utility model is as follows: the flue gas to be separated is pressurized and then is introduced into a balance kettle 15, the liquid participating in the hydration reaction is introduced into a hydration tower 18, in order to promote the hydration reaction of carbon dioxide, the liquid adopts a solution containing an accelerant, the traditional process adopts a mixed solution of the accelerant SDS and the accelerant THF, the foaming is serious during stirring, and the industrial recovery and the reutilization are not facilitated.
After the solution containing the accelerator is introduced into the hydration tower 18, the solution is pre-balanced at a temperature higher than the phase equilibrium temperature, after the solution is balanced for a period of time, the first valve 16 is opened, the flue gas with a certain pressure in the equilibrium kettle 15 is introduced into the hydration tower 18, and the solution is dissolved and stirred by the stirring mechanism 181 under the condition of the temperature higher than the phase equilibrium pressure. After the pressure remained stable, the stirring was stopped. The temperature of the hydration tower 18 is reduced, after the temperature is reduced to the reaction temperature, the stirring is started again, the pressure in the hydration tower 18 is reduced continuously, and solid CO is generated in the hydration tower 2 Hydrates while the other gases remain in the gaseous state. In the process, the temperature rise and the temperature drop are realized by a jacketed high-low temperature circulating condenser arranged on the outer wall of the hydration tower 18, and the circulating medium of the jacketed high-low temperature circulating condenser is ethylene glycol. In order to accurately control the temperature and pressure within hydration tower 18, the head of hydration tower 18 was fitted with a 0.25MPa dual range manometer and a 22.5MPa safety burst valve, while the temperature of hydration tower 18 was measured using a thermowell and a type K thermocouple. In order to reduce energy consumption, the outer wall of the hydration tower 18 is covered with heat insulation material, and the outside of the gas pipeline is also covered with heat insulation material.
After the hydration reaction is finished, the second valve 17 is opened, other gases in the flue gas can be discharged through the first exhaust pipe 183, according to the components of the gases, if the gases are pollution-free gases, the first exhaust pipe 183 can be directly communicated with the atmosphere, and if polluted gases or gases with recycling value exist, the first exhaust pipe 183 can be connected with a gas storage device. After the gas in the hydration tower 18 is exhausted, the second valve 17 is closed, and the third valve 19 is opened at the same time, and the heating is usedMechanism pair CO 2 The hydrate is heated to 298K (Kelvin), at which temperature CO is present 2 The hydrate is decomposed and changed into gaseous CO 2 Can enter the vapor collection canister 21 through the second exhaust pipe 184 and be stored in the vapor collection canister 21.
In order to realize the recycling of the accelerator solution and facilitate the supplement of the accelerator solution, the liquid discharge pipe 186 is connected with a liquid storage tank 25, the liquid inlet pipe 185 is communicated with the liquid storage tank 25, and the liquid inlet pipe 185 is provided with a liquid inlet pump 29. The liquid storage tank 25 stores an accelerator solution, the accelerator solution is a compound solution prepared by mixing carbon materials such as graphene oxide and acidified carbon nanotubes with an accelerator THF, and the accelerator solution can enter the hydration tower 18 through the liquid inlet pipe 185 again under the action of the liquid inlet pump 29, so that the reutilization is realized, and the production cost is reduced.
To facilitate detection of separated CO 2 The gas collecting tank 21 is connected with a gas chromatography detector 24 through a detection pipe 30, and the detection pipe 30 is provided with a sixth valve 22. Opening the sixth valve 22 and collecting CO in the gas tank 21 2 The CO flows to the gas chromatography detector 24 through the detection tube 30, and the gas chromatography detector 24 can detect the CO 2 Purity of the impurity gas and composition of the impurity gas. An automatic sampling valve is arranged between the detection tube 30 and the gas chromatography detector 24 for automatically analyzing CO in the flue gas on line 2 The separation efficiency.
The second exhaust pipe 184 is connected to a vacuum pump 23, and the vacuum pump 23 can pump out the residual gas in the hydration tower 18, so as to reduce the residual gas.
The bottom of the hydration tower 18 is provided with a sampling valve, and the sampling valve is connected with an in-situ pool. The sampling valve and the home position tank are not shown in fig. 1, the sampling valve can be a common ball valve, and the home position tank can be a conventional tank body. In CO 2 During the generation of hydrate, the sampling valve can be used for timing CO 2 Sampling the hydrate, opening the sampling valve, and then adding CO 2 The hydrate slurry flows into the in-situ pool, and CO can be observed 2 Microstructure of hydrate, judgment of CO 2 The hydrate formation rate.
The gas supply system can be a pipeline for collecting, cooling and pressurizing the flue gas generated by the power plant, and the device is used for treating the flue gas of the power plant.
In addition, the device can also be used for experiments to verify CO 2 The gas supply system then provides simulated flue gas and pressurizes the flue gas at this moment, specifically:
the gas supply system comprises a plurality of gas storage mechanisms, a condenser 9 and a mixing tank 11, each gas storage mechanism comprises a first gas cylinder 1 and a second gas cylinder 2, each first gas cylinder 1 and each second gas cylinder 2 are connected with the condenser 9 through a pipeline, each first gas cylinder 1 and a tenth valve 3, a first pressure reducing valve 5 and a first gas flow meter 7 are sequentially arranged on the pipeline between the condensers 9, and each second gas cylinder 2 and a eleventh valve 4, a second pressure reducing valve 6 and a second gas flow meter 8 are sequentially arranged on the pipeline between the condensers 9. The condenser 9 is connected with a mixing tank 11 through a pipeline, the mixing tank 11 is connected with a booster pump 13 through a pipeline, and the booster pump 13 is connected with a balance kettle 15 through a pipeline; a seventh valve 10 is arranged on a pipeline between the condenser 9 and the mixing tank 11, an eighth valve 12 is arranged on a pipeline between the mixing tank 11 and the booster pump 13, and a ninth valve 14 is arranged on a pipeline between the booster pump 13 and the balance kettle 15.
The mixed gas of different flue gas component concentrations is configured through the mixing tank 11. Generally, the components of the flue gas of the power plant are mainly nitrogen and carbon dioxide, wherein the nitrogen accounts for about 80% and the carbon dioxide accounts for about 20%, therefore, two gas cylinders are used for supplying gas, the first gas cylinder 1 is a nitrogen cylinder, the second gas cylinder 2 is a carbon dioxide cylinder, the tenth valve 3 and the eleventh valve 4 are opened, the nitrogen in the first gas cylinder 1 and the carbon dioxide in the second gas cylinder 2 can be respectively conveyed to the condenser 9 through different pipelines, the first pressure reducing valve 5 and the second pressure reducing valve 6 are used for controlling the gas pressure, and the first gas flow meter 7 and the second gas flow meter 8 are used for controlling the conveying amount of the gas, so that the ratio of the nitrogen to the carbon dioxide is ensured to be 4: 1. the condenser 9 cools the gas, opens the seventh valve 10, can get into the blending tank 11 with the gas after cooling, and nitrogen gas and carbon dioxide are evenly mixed in the blending tank 11. The eighth valve 12 is opened, the mixture of nitrogen and carbon dioxide is pressurized to 0.5MPa by the pressurizing pump 13, and then stored in the equilibrium kettle 15.
The other gases inevitably exist in the separated carbon dioxide, and in order to improve the purity of the carbon dioxide in the gas collecting tank 21, the gas collecting tank 21 is connected to the pressurizing pump 13 through a circulating pipe 31, and a twelfth valve 20 is provided on the circulating pipe 31. After the first separation and extraction, the ninth valve 14 is opened, the carbon dioxide in the gas collecting tank 21 can be pressurized again under the action of the pressure pump 13 and enters the equilibrium kettle 15, and then the carbon dioxide is introduced into the hydration tower 18 again for hydration reaction, and the gas which does not participate in the hydration reaction is discharged, so that the continuous separation and purification effects are achieved. The experiment proves that the concentration of the separated carbon dioxide can reach more than 98 percent.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A device that is arranged in hydrate method single-stage to catch carbon dioxide in separating flue gas in succession, its characterized in that: comprises a gas supply system, a balance kettle (15), a hydration tower (18), a gas collecting tank (21) and a jacketed high-low temperature circulating condenser for cooling or heating the hydration tower (18);
a stirring mechanism (181) is arranged in the hydration tower (18), an air inlet pipe (182), a first exhaust pipe (183), a second exhaust pipe (184) and a liquid inlet pipe (185) are arranged at the upper part of the hydration tower (18), and a liquid outlet pipe (186) is arranged at the bottom of the hydration tower (18); the balance kettle (15) is connected with the air inlet pipe (182), and the air inlet pipe (182) is provided with a first valve (16); a second valve (17) is arranged on the first exhaust pipe (183), the second exhaust pipe (184) is connected with the gas collecting tank (21), and a third valve (19) is arranged on the second exhaust pipe (184); a fourth valve (26) is arranged on the liquid inlet pipe (185), and a fifth valve (27) is arranged on the liquid outlet pipe (186).
2. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 1, characterized in that: the liquid discharge pipe (186) is connected with a liquid storage tank (25), the liquid inlet pipe (185) is communicated with the liquid storage tank (25), and a liquid inlet pump (29) is arranged on the liquid inlet pipe (185).
3. The device for single-stage continuous capturing and separating of carbon dioxide in flue gas by using the hydrate method according to claim 1, is characterized in that: the gas collecting tank (21) is connected with a gas chromatography detector (24) through a detection pipe (30), a sixth valve (22) is arranged on the detection pipe (30), and an automatic sampling valve is arranged between the detection pipe (30) and the gas chromatography detector (24).
4. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 1, characterized in that: the second exhaust pipe (184) is connected with a vacuum pump (23).
5. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 1, characterized in that: the gas supply system comprises a plurality of gas storage mechanisms, a condenser (9) and a mixing tank (11), the plurality of gas storage mechanisms are all connected with the condenser (9), the condenser (9) is connected with the mixing tank (11) through a pipeline, the mixing tank (11) is connected with a pressure pump (13) through a pipeline, and the pressure pump (13) is connected with the balance kettle (15) through a pipeline; be provided with seventh valve (10) on the pipeline between condenser (9) and blending tank (11), blending tank (11) with be provided with eighth valve (12) on the pipeline between force (forcing) pump (13), be provided with ninth valve (14) on the pipeline between force (forcing) pump (13) and reation kettle (15).
6. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 5, wherein: the gas storage mechanism comprises a first gas cylinder (1) and a second gas cylinder (2), the first gas cylinder (1) and the second gas cylinder (2) are connected with the condenser (9) through pipelines, a tenth valve (3), a first pressure reducing valve (5) and a first gas flow meter (7) are sequentially arranged on the pipeline between the first gas cylinder (1) and the condenser (9), and an eleventh valve (4), a second pressure reducing valve (6) and a second gas flow meter (8) are sequentially arranged on the pipeline between the second gas cylinder (2) and the condenser (9).
7. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 5 or 6, wherein: the gas collecting tank (21) is connected with the pressure pump (13) through a circulating pipe (31), and a twelfth valve (20) is arranged on the circulating pipe (31).
8. The device for single-stage continuous capture and separation of carbon dioxide in flue gas by the hydrate method according to claim 1, characterized in that: the stirring mechanism (181) is a magnetic coupling mechanical stirring paddle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221233066.1U CN217449626U (en) | 2022-05-20 | 2022-05-20 | Device for continuously capturing and separating carbon dioxide in flue gas by single stage through hydrate method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221233066.1U CN217449626U (en) | 2022-05-20 | 2022-05-20 | Device for continuously capturing and separating carbon dioxide in flue gas by single stage through hydrate method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217449626U true CN217449626U (en) | 2022-09-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221233066.1U Expired - Fee Related CN217449626U (en) | 2022-05-20 | 2022-05-20 | Device for continuously capturing and separating carbon dioxide in flue gas by single stage through hydrate method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217449626U (en) |
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2022
- 2022-05-20 CN CN202221233066.1U patent/CN217449626U/en not_active Expired - Fee Related
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