CN219482139U - Carbon trapping system suitable for two-phase absorbent - Google Patents
Carbon trapping system suitable for two-phase absorbent Download PDFInfo
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- CN219482139U CN219482139U CN202320597129.XU CN202320597129U CN219482139U CN 219482139 U CN219482139 U CN 219482139U CN 202320597129 U CN202320597129 U CN 202320597129U CN 219482139 U CN219482139 U CN 219482139U
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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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Abstract
The utility model discloses a carbon trapping system suitable for a two-phase absorbent, which comprises a gravity phase separator and a lean CO 2 Phase storage tank rich in CO 2 Phase storage tank, first pump, second pump and absorbent storage tank, gravity phase separator, first pump, lean CO 2 The phase storage tank and the absorbent storage tank are sequentially communicated, and the gravity phase separator, the second pump and the absorbent storage tank are rich in CO 2 The phase storage tank and the absorbent storage tank are sequentially communicated, a light phase outlet and a heavy phase outlet are arranged on the gravity phase separator, a first pipeline is arranged between the light phase outlet and the first pump, a first valve is arranged on the first pipeline, a second pipeline is arranged between the light phase outlet and the second pump, a second valve is arranged on the second pipeline, and the heavy phase outlet and the first pump are connected through a pipelineA third pipeline is arranged between the first pumps, a third valve is arranged on the third pipeline, a fourth pipeline is arranged between the heavy phase outlet and the second pump, and a fourth valve is arranged on the fourth pipeline, and the system can make CO rich according to the formula of the absorbent 2 Phase solution and lean CO 2 The flow rates of the phase solutions are matched with each other.
Description
Technical Field
The utility model is used in the technical field of carbon capture, and particularly relates to a carbon capture system suitable for a two-phase absorbent.
Background
Low CO for coal-fired power plant, steel, cement, etc 2 The carbon dioxide emission reduction of the concentrated flue gas can be carried out by adopting a chemical absorption method after combustion to collect carbon dioxide, at present, the most applied technology is a carbon collection technology using organic amine as an absorption liquid, wherein MEA is the earliest applied commercial carbon collection absorbent, and the carbon collection absorbent has the advantages of good absorption effect and low cost, but has the problems of high energy consumption, easy degradation, large corrosiveness and the like, and in recent years, various types of novel absorbents including mixed amine absorbents and two-phase absorption are proposedAgents, anhydrous absorbents, etc., to reduce carbon capture energy consumption and operating costs. Wherein the two-phase absorbent refers to absorption liquid for absorbing CO 2 After that, two immiscible lean COs are formed 2 Phase (CO) 2 Low content) and rich in CO 2 Liquid (CO) 2 High content), separating the two, and then only enriching the CO 2 The phase is circulated to a desorption tower for desorption, the process can not only improve the efficiency of the absorption process and the desorption process, but also effectively reduce the consumption of sensible heat and vaporization latent heat in the regeneration process, thereby reducing the cost of energy consumption, and two solutions with larger physical property difference are formed after the phase separation of the two-phase absorbent, wherein only CO is enriched 2 The liquid phase needs to be heated and desorbed for CO enrichment 2 Phase desorption is carried out before the phase is depleted of CO 2 The phase mixture forms a complete absorbent, the whole circulation process has great difference with the conventional single-phase amine absorbent, and the separation control of the two-phase absorbent in a phase separator is different due to the different phase separating agents of the two-phase absorbent, such as rich CO of MAE/sulfolane/water two-phase absorbent 2 The phase density is small and the phase is separated from the light phase outlet of the gravity phase separator, and the phase is rich in CO like AEEA/DEEA/water two-phase absorbent 2 The phase density is high and the phase is separated from the heavy phase outlet of the gravity phase separator, so that the existing two-phase absorbent process system does not reasonably consider the problem of adaptability of the two-phase absorbent type and cannot work by using different types of two-phase absorbent. In addition, the two-phase absorbent is rich in CO 2 Required and lean CO after phase desorption regeneration 2 The complete absorbent can be formed by mixing the phases again according to the formula proportion, and the existing two-phase absorbent process system does not consider the problem of effectively mixing and recycling the lean phase and the rich phase of the absorbent, so that the applicability is poor in practical operation control.
Disclosure of Invention
The present utility model aims to solve at least one of the technical problems in the prior art and to provide a carbon capture system suitable for two-phase absorbents, which can be adapted to different types of two-phase absorbents.
The technical scheme adopted for solving the technical problems is as follows:
carbon trapping system suitable for two-phase absorbent and bagGravity phase separator, lean CO 2 Phase storage tank rich in CO 2 A phase storage tank, a first pump, a second pump and an absorbent storage tank, said gravity phase separator, said first pump, said lean CO 2 The phase storage tank is sequentially communicated with the absorbent storage tank, and the gravity phase separator, the second pump and the CO-rich tank are sequentially communicated with each other 2 The phase storage tank is sequentially communicated with the absorbent storage tank, and the CO is rich 2 A phase storage tank is arranged between the second pump and the second pump for enriching CO 2 Conversion of the phase solution to CO 2 The carbon capture desorption device of looks lean solution, be equipped with light phase export and heavy phase export on the gravity phase separator, the light phase export with be equipped with first pipeline between the first pump, be equipped with first valve on the first pipeline, the light phase export with be equipped with the second pipeline between the second pump, be equipped with the second valve on the second pipeline, the heavy phase export with be equipped with the third pipeline between the first pump, be equipped with the third valve on the third pipeline, the heavy phase export with be equipped with the fourth pipeline between the second pump, be equipped with the fourth valve on the fourth pipeline.
Preferably, the first pump is lean in CO 2 A phase pump, the second pump is rich in CO 2 And (5) a phase pump.
Preferably, the lean CO 2 A third pump is arranged between the phase storage tank and the absorbent storage tank, and the CO-rich liquid is rich in CO 2 A fourth pump is arranged between the phase storage tank and the absorbent storage tank.
Preferably, the absorbent storage tank is provided with a first inlet and a second inlet, the third pump is communicated with the absorbent storage tank through the first inlet, the fourth pump is communicated with the absorbent storage tank through the second inlet, the absorbent storage tank is connected with a liquid supplementing pipe, and a stirrer is arranged in the absorbent storage tank.
Preferably, an absorption tower is arranged between the absorbent storage tank and the gravity phase separator, a fifth pump is arranged between the absorption tower and the absorbent storage tank, a first outlet is arranged on the absorbent storage tank, and the fifth pump is communicated with the absorbent storage tank through the first outlet.
Preferably, a cooler is arranged between the absorption tower and the fifth pump, and a sixth pump for conveying the absorbent rich liquid is arranged between the absorption tower and the gravity phase separator.
Preferably, the carbon capture desorption device comprises a carbon dioxide separator arranged on the carbon dioxide rich layer 2 A lean-rich liquid heat exchanger between the phase storage tank and the second pump.
Preferably, the carbon capturing and desorbing device comprises a desorber, and a device for inputting rich CO into the desorber is arranged between the desorber and the lean-rich liquid heat exchanger 2 A fifth line of phases and a means for withdrawing CO-rich from the desorber 2 And a sixth pipeline of the phase lean liquid, wherein a seventh pump is arranged on the sixth pipeline.
Preferably, a condenser and a gas-liquid separator are connected to the top of the desorption tower.
Preferably, the bottom of the desorption tower is connected with a reboiler.
One of the above technical solutions has at least one of the following advantages or beneficial effects: the carbon capture system suitable for two-phase absorbent is lean in CO 2 Phase storage tank for storing lean CO 2 Phase solution rich in CO 2 The phase storage tank is used for storing rich CO 2 Phase lean solution rich in CO 2 A phase storage tank and a second pump are arranged between the phase storage tank and the second pump for enriching CO 2 Conversion of the phase solution to CO 2 Carbon trapping and desorbing device for phase lean solution, wherein the carbon trapping and desorbing device mainly uses CO-rich gas 2 Phase solution heating pyrolysis CO sucking out 2 Forming rich CO 2 The lean liquid can be used for lean CO 2 The phase solution is remixed into absorbent for capturing carbon in flue gas, the gravity phase separator separates by gravity, namely, the density difference of two immiscible liquid phases can be utilized for separation, the heavy phase with high density is discharged from a heavy phase outlet, the light phase with low density is discharged from a light phase outlet, and the absorbent is rich in CO 2 When the phase is heavy phase, the heavy phase outlet of the gravity phase separator is used for conveying the rich CO through the second pump 2 The phase, gravity phase separator light phase outlet delivers lean CO by a first pump 4 2 A phase; rich in CO as absorbent 2 When the phase is light phase, the heavy phase outlet of the gravity phase separator is used for conveying and conveying lean CO through the first pump 4 2 The phase, the light phase outlet of the gravity phase separator is pumped by a second pumpWeight-feeding CO 2 Phase, controlled CO lean for a two-phase absorbent carbon capture system 2 Phase solution and rich CO 2 The phase lean liquid is respectively lean in CO 2 Phase storage tank and rich in CO 2 The phase storage tank enters the absorbent storage tank so as to restore the two phases to the original proportion of the absorbent, and the absorbent storage tank is rich in CO 2 The phase solution passing through the carbon capture desorption device needs to go through a longer desorption flow to be returned to the absorbent storage tank, which inevitably results in more rich CO 2 The phase solution resides in the desorption flow, so the carbon trapping system suitable for the two-phase absorbent is provided with lean CO 2 Phase storage tank and rich in CO 2 The phase storage tank is regulated according to the composition of the absorbent formulation by lean CO 2 Phase storage tank and rich in CO 2 A phase storage tank for enriching CO 2 Phase solution and lean CO 2 The flow rates of the phase solutions are matched to each other, thereby solving the compatibility and operational reliability of the two-phase absorbent system.
Additional aspects and advantages of the utility model will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the utility model.
Drawings
The foregoing and/or additional aspects and advantages of the utility model will become apparent and may be better understood from the following description of embodiments taken in conjunction with the accompanying drawings in which:
fig. 1 is a schematic diagram of the structure of an embodiment of the present utility model.
Detailed Description
Reference will now be made in detail to the present embodiments of the present utility model, examples of which are illustrated in the accompanying drawings, wherein the accompanying drawings are used to supplement the description of the written description so that one can intuitively and intuitively understand each technical feature and overall technical scheme of the present utility model, but not to limit the scope of the present utility model.
In the present utility model, if directions (up, down, left, right, front and rear) are described, they are merely for convenience of description of the technical solution of the present utility model, and do not indicate or imply that the technical features must be in a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
In the present utility model, "a plurality of" means one or more, and "a plurality of" means two or more, and "greater than", "less than", "exceeding", etc. are understood to not include the present number; "above", "below", "within" and the like are understood to include this number. In the description of the present utility model, the description of "first" and "second" if any is used solely for the purpose of distinguishing between technical features and not necessarily for the purpose of indicating or implying a relative importance or implicitly indicating the number of technical features indicated or implicitly indicating the precedence of the technical features indicated.
In the present utility model, unless clearly defined otherwise, terms such as "disposed," "mounted," "connected," and the like should be construed broadly and may be connected directly or indirectly through an intermediate medium, for example; the connecting device can be fixedly connected, detachably connected and integrally formed; can be mechanically connected, electrically connected or capable of communicating with each other; may be a communication between two elements or an interaction between two elements. The specific meaning of the words in the utility model can be reasonably determined by a person skilled in the art in combination with the specific content of the technical solution.
Embodiments of the present utility model provide a carbon capture system suitable for use with a two-phase absorbent, see FIG. 1, comprising a gravity phase separator 1, lean in CO 2 Phase storage tank 2, rich in CO 2 A phase storage tank 3, a first pump 4, a second pump 5 and an absorbent storage tank 6, lean in CO 2 The phase storage tank 2 is used for storing lean CO 2 Phase solution rich in CO 2 The phase storage tank 3 is used for storing rich CO 2 Phase lean liquid, gravity phase separator 1, first pump 4, lean CO 2 The phase storage tank 2 and the absorbent storage tank 6 are sequentially communicated, and the gravity phase separator 1, the second pump 5 and the CO-rich tank are respectively arranged 2 The phase storage tank 3 and the absorbent storage tank 6 are sequentially communicated and are rich in CO 2 A phase storage tank 3 and a second pump 5 are arranged between the two pumps for enriching CO 2 Conversion of the phase solution to CO 2 Carbon trapping and desorbing device for phase lean solution, wherein the carbon trapping and desorbing device mainly uses CO-rich gas 2 Phase solution heating pyrolysis sucking CO 2 Forming rich CO 2 The lean liquid can be used for lean CO 2 The phase solution is remixed into absorbent for capturing carbon in flue gas, the gravity phase separator 1 is provided with a light phase outlet and a heavy phase outlet, a first pipeline is arranged between the light phase outlet and the first pump 4, a first valve 7 is arranged on the first pipeline, a second pipeline is arranged between the light phase outlet and the second pump 5, a second valve 8 is arranged on the second pipeline, a third pipeline is arranged between the heavy phase outlet and the first pump 4, a third valve 9 is arranged on the third pipeline, a fourth pipeline is arranged between the heavy phase outlet and the second pump 5, a fourth valve 10 is arranged on the fourth pipeline, the gravity phase separator 1 performs phase separation by gravity, the density difference of two immiscible liquid phases can be utilized for separation, the heavy phase with high density is discharged from the heavy phase outlet, the light phase with low density is discharged from the light phase outlet, and when the absorbent is rich in CO 2 When the phase is heavy phase, the second valve 8 and the third valve 9 are closed, the first valve 7 and the fourth valve 10 are opened, and at the moment, the heavy phase outlet of the gravity phase separator 1 is used for conveying the rich CO through the second pump 5 2 The light phase outlet of the gravity phase separator 1 is used for conveying lean CO through a first pump 4 2 A phase; rich in CO as absorbent 2 When the phase is light phase, the first valve 7 and the fourth valve 10, the second valve 8 and the third valve 9 are opened, and the heavy phase outlet of the gravity phase separator 1 is used for conveying lean CO through the first pump 4 2 The phase, at this time the light phase outlet of the gravity phase separator 1 is fed with CO-rich gas by the second pump 5 2 Phase, the carbon capture system suitable for the two-phase absorbent is rich in CO 2 The phase solution, which passes through the carbon capture desorption device, needs to go through a longer desorption process to be returned to the absorbent tank 6, which inevitably results in a greater enrichment of CO 2 The phase solution resides in the desorption scheme and is lean in CO 2 Phase and CO-rich 2 The phase lean solution is mixed according to the formula proportion to form the complete absorbent, so the carbon trapping system suitable for the two-phase absorbent is provided with the lean CO 2 Phase storage tank 2 and rich in CO 2 The phase storage tank 3 is regulated according to the composition of the absorbent formulation by controlling the lean CO 2 Phase solution and rich CO 2 The phase lean liquid is respectively lean in CO 2 Phase storage tank 2 and rich in CO 2 The proportion of the flow of the phase storage tank 3 into the absorbent storage tank 6, so that the two phases are restored to the absorbentOriginal proportioning is adopted, so that the compatibility and the operation reliability of the two-phase absorbent system are solved.
It will be appreciated that the gravity phase separator 1 is provided with a liquid measuring point, when the heavy phase outlet liquid level and the light phase outlet liquid level reach the design range, the first pump 4 and the second pump 5 are started, if the heavy phase outlet liquid level or the light phase outlet liquid level of the liquid level measuring point is lower than the lower limit warning value, the first pump 4 and the second pump 5 are stopped, and if the heavy phase outlet liquid level or the light phase outlet liquid level is higher than the upper limit warning value, the first pump 4 or the second pump 5 increases the flow output.
As a preferred embodiment of the utility model, the first pump 4 is CO-lean 2 The phase pump and the second pump 5 are rich in CO 2 And (5) a phase pump.
Referring to FIG. 1, lean CO 2 A third pump 11 is arranged between the phase storage tank 2 and the absorbent storage tank 6, and is rich in CO 2 A fourth pump 12 is arranged between the phase storage tank 3 and the absorbent storage tank 6, and the third pump 11 and the fourth pump 12 are linked according to the formula composition of the absorbent to respectively convey lean CO according to the appointed proportion 2 Lean CO in phase storage tank 2 2 Phase solution and rich CO 2 CO-rich in the phase storage tank 3 2 The phase lean liquid is fed to the absorbent storage tank 6, where, as will be appreciated, it is lean in CO 2 The level of the level gauge in the phase tank 2 rises to the design range and the third pump 11 is started, if it is CO lean 2 The third pump 11 is stopped if the liquid level of the liquid level measuring point 3 in the phase storage tank 2 is lower than the lower limit warning value, if the liquid level is lean in CO 2 The liquid level height of the liquid level measuring point 3 in the phase storage tank 2 is higher than the liquid level upper limit warning value, and the third pump 11 increases the flow output; when rich in CO 2 The liquid level of the liquid level measuring point in the phase storage tank 3 rises to the design range, and the fourth pump 12 is started, if the phase storage tank is rich in CO 2 The level of the liquid level measuring point in the phase storage tank 3 is lower than the lower limit warning value, and the fourth pump 12 is stopped, if the liquid level is rich in CO 2 The liquid level height of the liquid level measuring point in the phase storage tank 3 is higher than the liquid level upper limit warning value, and the fourth pump 12 increases the flow output.
In some embodiments, the absorbent storage tank 6 is provided with a first inlet and a second inlet, the third pump 11 is communicated with the absorbent storage tank 6 through the first inlet, the fourth pump 12 is communicated with the absorbent storage tank 6 through the second inlet, the absorbent storage tank 6 is connected with a liquid supplementing pipe 13, and a stirrer is arranged in the absorbent storage tank 6.
Referring to fig. 1, an absorption tower 14 is arranged between the absorbent storage tank 6 and the gravity phase separator 1, a fifth pump 15 is arranged between the absorption tower 14 and the absorbent storage tank 6, a first outlet is arranged on the absorbent storage tank 6, and the fifth pump 15 is communicated with the absorbent storage tank 6 through the first outlet.
Referring to fig. 1, a cooler 16 is provided between the absorption tower 14 and the fifth pump 15, a sixth pump 17 for transporting the absorbent rich liquid is provided between the absorption tower 14 and the gravity phase separator 1, and when the liquid level height of the liquid level measuring point in the absorbent storage tank 6 is lower than the lower limit warning value, the sixth pump 17 stops running.
As a preferred embodiment of the present utility model, the carbon capture desorption apparatus comprises a carbon capture desorption apparatus provided at a CO-rich site 2 A lean-rich liquid heat exchanger 18 between the phase storage tank 3 and the second pump 5.
In some embodiments, the carbon capture desorption device comprises a desorption tower 19, and a CO-rich input device for inputting CO into the desorption tower 19 is arranged between the desorption tower 19 and the lean-rich liquid heat exchanger 18 2 A fifth line for the phase and for the export of CO-rich from the desorber 19 2 A sixth pipeline of the phase lean solution, a seventh pump 20 is arranged on the sixth pipeline, and CO is desorbed from the desorption tower 19 2 Formation of CO-rich 2 The phase lean solution is collected at the bottom of the desorption tower, when the liquid level of the liquid level measuring point at the bottom of the desorption tower rises to the design range, the seventh pump 20 is started, if the liquid level of the liquid level measuring point at the bottom of the absorption tower 19 is lower than the lower limit warning value, the seventh pump 20 is stopped, if the liquid level of the liquid level measuring point at the bottom of the desorption tower 19 is higher than the upper limit warning value, the seventh pump 20 increases the flow output, and the desorbed rich CO is obtained 2 The phase lean liquid is conveyed to rich CO through a lean-rich liquid heat exchanger 18 2 And a phase storage tank 3.
Referring to fig. 1, a condenser 21 and a gas-liquid separator 22 are connected to the top of the desorption column 19.
In some embodiments, a reboiler 23 is connected to the bottom of the desorber 19.
In some embodiments, ultra low emission flue gas (65 ten thousand Nm) 3 /h，CO 2 Concentration of 12 vol%) is washed by pretreatment tower and cooled to about 40 deg.CThen enters the absorption tower 14 from the bottom inlet of the absorption tower 14 to react with MAE/sulfolane two-phase absorbent entering from the upper inlet of the absorption tower 14 (absorbent flow is about 2000 m) 3 The operating temperature of the absorption tower 14 is distributed between 50 and 60 ℃, the operating pressure is normal pressure, and the operating temperature is CO at 40 ℃ 2 Is absorbed into absorbent to form two miscible solution rich phases, which are conveyed to the gravity phase separator 1 by a sixth pump 17 to be separated into organic phase and aqueous phase, wherein the organic phase is rich in sulfolane and is lean in CO 2 The heavy phase (volume proportion is 45%) and the aqueous phase is rich in CO 2 The second valve 8 and the third valve 9 are closed, the first valve 7 and the fourth valve 10 are opened, and the CO is lean (55% by volume) 2 The phase is fed to the lean CO via a first pump 4 2 A phase storage tank 2; rich in CO 2 The phase is conveyed by a second pump 5 to be heated by a lean-rich liquid heat exchanger 18, then the temperature is raised to 100-105 ℃, the pressure is 4-5 bar, then the phase enters a desorption tower 19 from the upper end of the desorption tower 19, the pressure in the desorption tower 19 is normal pressure, the temperature at the bottom of the desorption tower 19 is controlled to be 110-120 ℃, and the phase is rich in CO 2 Vapor generated by a reboiler 23 is heated to form stripping gas, the stripping gas is discharged from the top of the stripping tower 19, and CO is formed after passing through a heat exchanger 3, a condenser 21 and a gas-liquid separator 22 2 The product gas and condensate are re-injected into the desorption tower 19, the heat source of the reboiler 23 is the steam provided by public engineering, the temperature is saturated steam above 130 ℃, the steam forms steam condensate after phase change heat release in the reboiler 23, and the bottom of the desorption tower 19 is rich in CO at high temperature generated by the reboiler 23 2 The phase lean liquid is conveyed to a lean-rich liquid heat exchanger 18 through a seventh pump 20 to heat rich CO 2 Phase, at the same time rich in CO 2 The temperature of the phase lean solution is reduced, heat is recovered, and then CO is enriched 2 The phase lean solution enters into rich CO 2 In the phase storage tank 3, the flow of the third pump 11 and the fourth pump 12 is controlled such that the lean CO is returned to the absorbent storage tank 2 Phase (flow rate about 980 m) 3 /h,52 ℃ and CO-rich 2 Lean solution (flow about 1200 m) 3 And/h, 57 ℃) can be mixed to the desired absorbent before further recirculation into the absorption column 14.
In the description of the present specification, reference to the terms "example," "embodiment," or "some embodiments," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the utility model. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The present utility model is, of course, not limited to the above-described embodiments, and one skilled in the art can make equivalent modifications or substitutions without departing from the spirit of the utility model, and these equivalent modifications or substitutions are intended to be included in the scope of the present utility model as defined in the claims.
Claims (10)
1. A carbon capture system suitable for use with a two-phase absorbent, characterized by: comprising a gravity phase separator, lean in CO 2 Phase storage tank rich in CO 2 A phase storage tank, a first pump, a second pump and an absorbent storage tank, said gravity phase separator, said first pump, said lean CO 2 The phase storage tank is sequentially communicated with the absorbent storage tank, and the gravity phase separator, the second pump and the CO-rich tank are sequentially communicated with each other 2 The phase storage tank is sequentially communicated with the absorbent storage tank, and the CO is rich 2 A phase storage tank is arranged between the second pump and the second pump for enriching CO 2 Conversion of the phase solution to CO 2 The carbon capture desorption device of looks lean solution, be equipped with light phase export and heavy phase export on the gravity phase separator, the light phase export with be equipped with first pipeline between the first pump, be equipped with first valve on the first pipeline, the light phase export with be equipped with the second pipeline between the second pump, be equipped with the second valve on the second pipeline, the heavy phase export with be equipped with the third pipeline between the first pump, be equipped with the third valve on the third pipeline, the heavy phase export with be equipped with the fourth pipeline between the second pump, be equipped with the fourth valve on the fourth pipeline.
2. The carbon capture system suitable for use with a two-phase absorbent of claim 1, wherein: the first pump is lean in CO 2 Phase pump, provided withThe second pump is rich in CO 2 And (5) a phase pump.
3. The carbon capture system suitable for use with a two-phase absorbent of claim 1, wherein: the lean CO 2 A third pump is arranged between the phase storage tank and the absorbent storage tank, and the CO-rich liquid is rich in CO 2 A fourth pump is arranged between the phase storage tank and the absorbent storage tank.
4. A carbon capture system suitable for use with a two-phase absorbent according to claim 3, wherein: be equipped with first entry and second entry on the absorbent storage tank, the third pump pass through first entry with the absorbent storage tank is linked together, the fourth pump pass through the second entry with the absorbent storage tank is linked together, be connected with the fluid replacement pipe on the absorbent storage tank, be equipped with the agitator in the absorbent storage tank.
5. The carbon capture system suitable for use with a two-phase absorbent of claim 1, wherein: an absorption tower is arranged between the absorbent storage tank and the gravity phase separator, a fifth pump is arranged between the absorption tower and the absorbent storage tank, a first outlet is arranged on the absorbent storage tank, and the fifth pump is communicated with the absorbent storage tank through the first outlet.
6. The carbon capture system suitable for use with a two-phase absorbent of claim 5, wherein: a cooler is arranged between the absorption tower and the fifth pump, and a sixth pump for conveying the absorbent rich liquid is arranged between the absorption tower and the gravity phase separator.
7. The carbon capture system suitable for use with a two-phase absorbent of claim 1, wherein: the carbon capture desorption device comprises a carbon dioxide gas generator arranged on the CO-rich part 2 A lean-rich liquid heat exchanger between the phase storage tank and the second pump.
8. The method according to claim 7, suitable for two phasesThe carbon trapping system of the absorbent is characterized in that: the carbon capturing and desorbing device comprises a desorber, wherein a device for inputting rich CO into the desorber is arranged between the desorber and the lean-rich liquid heat exchanger 2 A fifth line of phases and a means for withdrawing CO-rich from the desorber 2 And a sixth pipeline of the phase lean liquid, wherein a seventh pump is arranged on the sixth pipeline.
9. The carbon capture system suitable for use with a two-phase absorbent of claim 8, wherein: the top of the desorption tower is connected with a condenser and a gas-liquid separator.
10. The carbon capture system suitable for use with a two-phase absorbent of claim 8, wherein: and the bottom of the desorption tower is connected with a reboiler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202320597129.XU CN219482139U (en) | 2023-03-23 | 2023-03-23 | Carbon trapping system suitable for two-phase absorbent |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320597129.XU CN219482139U (en) | 2023-03-23 | 2023-03-23 | Carbon trapping system suitable for two-phase absorbent |
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| CN219482139U true CN219482139U (en) | 2023-08-08 |
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| CN202320597129.XU Active CN219482139U (en) | 2023-03-23 | 2023-03-23 | Carbon trapping system suitable for two-phase absorbent |
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