Flue gas carbon dioxide trapping and sealing system

Abstract

The invention provides a flue gas carbon dioxide capturing and sealing system, which comprises an absorption tower, a regeneration tower, a separator, a sealing unit and an absorption refrigerator, the absorption tower is provided with a flue gas inlet for introducing flue gas, the regeneration tower is connected with the absorption tower, and the separator is connected with the absorption refrigerator. An absorbent in the absorption tower reacts with flue gas to form a saturated absorbent, the saturated absorbent is introduced into the regeneration tower, the regeneration tower is used for desorbing the saturated absorbent and then introducing the saturated absorbent into the absorption tower, the separator is connected with the regeneration tower, the sealing unit comprises a compression assembly and a drying assembly, the compression assembly is connected with the separator, and the drying assembly is connected with the compression assembly. The drying assembly comprises a drying tower and a heater, the heater is connected with the drying tower, a hot side inlet of the absorption refrigerator is connected with a steam outlet of the heater, and a cold side outlet of the absorption refrigerator is connected with at least one of the separator and the absorption tower. The flue gas carbon dioxide trapping and sealing system is high in energy utilization rate and low in overall consumption.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon dioxide capture, and in particular to a flue gas carbon dioxide capture and storage system. Background Art

[0002] Carbon dioxide is one of the main components of greenhouse gases that cause global warming, and coal-fired power plants are the largest industry emitting carbon dioxide. In addition to causing global warming, carbon dioxide can also be used as a chemical raw material, and the captured and purified carbon dioxide can also be injected into oil layers in a supercritical state to increase oil recovery. It can be predicted that with the development and improvement of capture technology and the continuous expansion of its application scope, carbon dioxide will become an important resource for improving oil field development effects and increasing crude oil recovery in my country.

[0003] At present, the carbon dioxide capture and purification process is still mainly based on absorption towers and desorption towers, using alcohol amine solution as absorbent. After chemical absorption and desorption, high-purity carbon dioxide gas is obtained. The main energy consumption in the process is the reboiler at the bottom of the desorption tower, which uses water vapor to heat the rich liquid to desorb carbon dioxide. In the absorption and desorption process, energy is not fully utilized in many places, resulting in low energy utilization. Summary of the invention

[0004] The present invention aims to solve at least one of the technical problems in the related art to a certain extent. To this end, an embodiment of the present invention provides a flue gas carbon dioxide capture and storage system, which has high energy utilization rate and low overall consumption.

[0005] The flue gas carbon dioxide capture and storage system of the embodiment of the present invention comprises:

[0006] An absorption tower, wherein the absorption tower has a flue gas inlet, and the flue gas inlet is used to introduce the pretreated flue gas;

[0007] A regeneration tower, the regeneration tower is connected to the absorption tower, the absorbent in the absorption tower reacts with the flue gas to form a saturated absorbent and is passed into the regeneration tower, the regeneration tower is used to desorb the saturated absorbent and then pass it into the absorption tower;

[0008] A separator, the separator is connected to the regeneration tower so that the regeneration gas discharged from the regeneration tower is separated into gas and liquid in the separator;

[0009] A sealing unit, the sealing unit comprising a compression component and a drying component, the compression component is connected to the separator to compress the gas discharged from the separator, and the drying component is connected to the compression component to dry part of the gas in the compression component,

[0010] The drying assembly includes a drying tower and a heater, wherein the heater is connected to the drying tower to heat the desiccant discharged from the drying tower and then pass the desiccant into the drying tower after being heated;

[0011] An absorption refrigerator, wherein a hot side inlet of the absorption refrigerator is connected to a vapor outlet of the heater, and a cold side outlet of the absorption refrigerator is connected to at least one of the separator and the absorption tower.

[0012] The flue gas carbon dioxide capture and storage system of the embodiment of the present invention can use the excess heat generated by the storage unit as the driving heat source of the absorption refrigerator, and then pass the cold energy generated by the absorption refrigerator into the separator and / or absorption tower to realize the utilization of the cold energy, thereby improving the energy utilization rate of the system and reducing the energy loss of the overall system.

[0013] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a lean-rich liquid heat exchanger, which is connected to both the absorption tower and the regeneration tower, so that the saturated absorbent discharged from the absorption tower and the desorbed absorbent discharged from the regeneration tower can exchange heat, and the desorbed absorbent is used to pass into the absorption tower, and the saturated absorbent is used to pass into the regeneration tower.

[0014] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a preheating heat exchanger, and the absorber includes a first spray section, a second spray section and a third spray section arranged in sequence along the flue gas flow direction, the first spray section, the second spray section and the third spray section are respectively connected to the first spray pipeline, the second spray pipeline and the third spray pipeline, the second spray pipeline has a rich liquid outlet, and the rich liquid outlet is connected to the lean and rich liquid heat exchanger through a rich liquid pipeline, and the preheating heat exchanger is connected to the first spray pipeline and the rich liquid pipeline, so that the rich liquid pipeline and the first spray pipeline exchange heat in the preheating heat exchanger.

[0015] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a phase separator, which has a phase separation inlet, a first phase separation outlet and a second phase separation outlet, the phase separation inlet is connected to the rich liquid outlet, the first phase separation outlet is connected to the spray inlet of the second spray section, and the second phase separation outlet is connected to the rich liquid pipeline.

[0016] In some embodiments, a cooler is provided on the third spray pipeline, and the cooling outlet of the absorption refrigerator is connected to the cooler.

[0017] In some embodiments, the third spray pipeline has an absorbent liquid discharge port, and the absorbent liquid discharge port is connected to the regeneration tower.

[0018] In some embodiments, the separator has a regeneration gas inlet, the regeneration gas outlet of the regeneration tower is connected to the regeneration gas inlet, and the cooling outlet of the absorption refrigerator is connected to the regeneration gas inlet.

[0019] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a regeneration water cooler, the hot side inlet of the regeneration water cooler is connected to the regeneration gas outlet of the regeneration tower, the hot side outlet of the regeneration water cooler is connected to the regeneration gas inlet, and the cold side inlet of the regeneration water cooler is connected to the cooling outlet of the absorption chiller.

[0020] In some embodiments, the separator also has a separation liquid outlet, and the third spray pipeline also has an absorbent inlet, the absorbent inlet is located downstream of the absorbent discharge port, and the absorbent inlet is located upstream of the cooler, and the separation liquid outlet is connected to the absorbent inlet.

[0021] In some embodiments, the third spray pipeline is further provided with a mixer, and the mixer is connected to the separation liquid outlet. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a schematic diagram of the structure of a flue gas carbon dioxide capture and storage system according to an embodiment of the present invention.

[0023] Reference numerals:

[0024] 1. Absorption tower, 11. First spray section, 12. Second spray section, 13. Third spray section, 14. Flue gas inlet,

[0025] 2. Regeneration tower,

[0026] 3. Separator, 31. Regeneration gas inlet, 32. Separation liquid outlet,

[0027] 4. Sealing unit, 41. Compression assembly, 42. Drying assembly, 421. Drying tower, 422. Heater,

[0028] 5. Absorption refrigeration machine,

[0029] 6. Lean and rich liquid heat exchanger,

[0030] 7. Preheat the heat exchanger,

[0031] 81. First spray pipeline, 82. Second spray pipeline, 83. Third spray pipeline, 831. Absorbent liquid discharge port, 832. Absorbent liquid inlet, 84. Cooler, 85. Mixer,

[0032] 9. Phase splitter,

[0033] 10. Regeneration water cooler. DETAILED DESCRIPTION

[0034] Embodiments of the present invention are described in detail below, and examples of the embodiments are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to be used to explain the present invention, but should not be understood as limiting the present invention.

[0035] like Figure 1 As shown, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention includes: an absorption tower 1, a regeneration tower 2, a separator 3, a storage unit 4 and an absorption refrigerator 5.

[0036] The absorption tower 1 has a flue gas inlet 14, and the flue gas inlet 14 is used to pass the pre-treated flue gas. The regeneration tower 2 is connected to the absorption tower 1. The absorbent in the absorption tower 1 reacts with the flue gas to form a saturated absorbent and passes it into the regeneration tower 2. The regeneration tower 2 is used to desorb the saturated absorbent and then pass it into the absorption tower 1. The separator 3 is connected to the regeneration tower 2 so that the regeneration gas discharged from the regeneration tower 2 is separated into gas and liquid in the separator 3. The sealing unit 4 includes a compression component 41 and a drying component 42. The compression component 41 is connected to the separator 3 to compress the gas discharged from the separator 3. The drying component 42 is connected to the compression component 41 to dry part of the gas in the compression component 41. The drying component 42 includes a drying tower 421 and a heater 422. The heater 422 is connected to the drying tower 421 to heat the desiccant discharged from the drying tower 421, and then pass the desiccant into the drying tower 421 after heating. The hot side inlet of the absorption refrigerator 5 is connected to the vapor outlet of the heater 422 , and the cold side outlet of the absorption refrigerator 5 is connected to at least one of the separator 3 and the absorption tower 1 .

[0037] Specifically, Figure 1 As shown, the flue gas discharged from the boiler usually contains a large amount of impurities, such as solid particles, etc. The flue gas can be pretreated before entering the absorption tower 1, wherein the pretreatment of the flue gas includes dust removal, cooling and other steps to ensure that the flue gas can better react with the absorbent when entering the absorption tower 1. The flue gas enters the absorption tower 1, and the absorbent is sprayed into the absorption tower 1, so that the absorbent reacts chemically with the pollutants (such as sulfur dioxide or nitrogen oxides) in the flue gas in the absorption tower 1 to form a saturated solution. These saturated solutions are then transported to the regeneration tower 2. In the regeneration tower 2, the pollutants are desorbed by physical or chemical methods, so that the absorbent can be regenerated and recycled. Optionally, the absorbent can be an organic amine solution.

[0038] The separator 3 may be a gas-liquid separation device, which is connected to the regeneration tower 2 to separate the liquid component (saturated solution carried by the absorbent) and the gas component in the regeneration gas discharged from the regeneration tower 2. In this way, the regenerated absorbent can be returned to the absorption tower 1 dryly, while the gas can be discharged or further processed.

[0039] The compression assembly 41 is used to increase the pressure of the low-pressure gas (regeneration gas carrying water vapor) discharged from the separator 3 for further processing or storage. The drying assembly 42 is used to remove moisture from the compressed gas to ensure the dryness of the gas and provide necessary conditions for subsequent storage.

[0040] The hot side inlet of the absorption refrigerator 5 is connected to the steam outlet of the heater 422, so that the high temperature steam generated by the heater 422 is used as a driving heat source to drive the refrigerator to work. The cold side outlet of the refrigerator can be connected to the separator 3, or to the absorption tower 1, or to both the separator 3 and the absorption tower 1, so as to provide the required cooling capacity for the separator 3 and the absorption tower 1 and reduce the use of external energy.

[0041] That is to say, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention can use the excess heat generated by the storage unit 4 as the driving heat source of the absorption refrigerator 5, and then pass the cold energy generated by the absorption refrigerator 5 into the separator 3 and / or the absorption tower 1 to realize the utilization of the cold energy, thereby improving the energy utilization rate of the system and reducing the energy loss of the overall system.

[0042] Therefore, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention not only utilizes the waste heat generated by the system, but also provides the cooling capacity required by the system, thereby achieving efficient utilization of energy and reducing the consumption of external energy.

[0043] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a lean-rich liquid heat exchanger 6, which is connected to both the absorption tower 1 and the regeneration tower 2, so that the saturated absorbent discharged from the absorption tower 1 and the desorbed absorbent discharged from the regeneration tower 2 can be heat exchanged, and the desorbed absorbent is used to pass into the absorption tower 1, and the saturated absorbent is used to pass into the regeneration tower 2.

[0044] It is understood that in the absorption tower 1, the flue gas reacts chemically with the sprayed absorbent, and the absorbent absorbs the pollutants (such as sulfur dioxide or nitrogen oxides) in the flue gas to form a saturated solution. The saturated absorbent is then discharged from the absorption tower 1 and flows into the lean-rich liquid heat exchanger 6.

[0045] In the heat exchanger, the saturated absorbent (rich liquid) exchanges heat with the unsaturated absorbent (lean liquid) from the regeneration tower 2. The heat in the rich liquid is transferred to the lean liquid, causing the temperature of the lean liquid to rise while the temperature of the rich liquid to fall. After the heat exchange, the lean liquid absorbs more heat, and its absorption capacity is enhanced, so it can enter the absorption tower 1 again to absorb more pollutants. As the rich liquid releases heat, its saturation decreases, and it becomes a relatively lean absorbent before entering the regeneration tower 2, making it easier to release the absorbed pollutants.

[0046] That is to say, after the rich liquid discharged from the absorption tower 1 and the lean liquid discharged from the regeneration tower 2 pass through the lean-rich liquid heat exchanger 6, the heat of the saturated absorbent discharged from the absorption tower 1 is effectively utilized, so that the absorbent discharged from the regeneration tower 2 can continue to absorb pollutants after passing into the absorption tower 1, thereby improving the efficiency of the entire system. As a result, not only the energy consumption of the system is reduced, but also the reaction of the lean liquid and the rich liquid passing into the absorption tower 1 and the regeneration tower 2 respectively is optimized, and the consumption of the absorbent is reduced, and its service life is extended.

[0047] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a preheating heat exchanger 7, and the absorber includes a first spray section 11, a second spray section 12 and a third spray section 13 arranged in sequence along the flue gas flow direction, the first spray section 11, the second spray section 12 and the third spray section 13 are respectively connected to the first spray pipeline 81, the second spray pipeline 82 and the third spray pipeline 83, the second spray pipeline 82 has a rich liquid outlet, and the rich liquid outlet is connected to the lean-rich liquid heat exchanger 6 through a rich liquid pipeline, and the preheating heat exchanger 7 is connected to the first spray pipeline 81 and the rich liquid pipeline, so that the rich liquid pipeline and the first spray pipeline 81 exchange heat in the preheating heat exchanger 7.

[0048] Specifically, Figure 1 As shown, the first spray section 11, the second spray section 12 and the third spray section 13 are arranged in sequence from bottom to top, and the first spray pipeline 81, the second spray pipeline 82 and the third spray pipeline 83 are all provided with spray pumps. The spray pumps can be used to spray the absorbent into the absorption tower 1, and the absorbent can also circulate between the absorption tower 1 and the spray pipelines.

[0049] It can be understood that, through the sequential arrangement of multiple spray sections, the flue gas temperature changes in a gradient (i.e., the temperature gradually decreases with increasing height), and the flue gas and the absorbent have more sufficient contact opportunities, thereby improving the absorbent's absorption efficiency of flue gas pollutants. Among them, the flue gas undergoes the first removal reaction in the first spray section 11, and the absorbent after the reaction has more impurities and a low recycling rate. The absorbent after the reaction can be passed into the power plant wastewater treatment system for treatment; and the absorbent in the second spray section 12 reacts with the flue gas to form a saturated absorbent (rich liquid), which is passed into the regeneration tower 2 for regeneration, and the absorbent can be reused.

[0050] That is to say, before the absorbent after reacting with the flue gas in the second spray section 12 is passed into the lean-rich liquid heat exchanger 6, the absorbent after reacting with the flue gas discharged from the first spray section 11 and the absorbent after reacting with the flue gas discharged from the second spray section 12 can be heat exchanged in the preheating heat exchanger 7, thereby ensuring the temperature of the absorbent discharged from the second spray section 12 during transportation, realizing heat recovery, and also improving the efficiency of absorbent regeneration.

[0051] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a phase separator 9, which has a phase separation inlet, a first phase separation outlet and a second phase separation outlet. The phase separation inlet is connected to the rich liquid outlet, the first phase separation outlet is connected to the spray inlet of the second spray section 12, and the second phase separation outlet is connected to the rich liquid pipeline.

[0052] Specifically, Figure 1 As shown, the second phase separation outlet is located at the bottom of the phase separator 9, and the phase separator 9 is connected to the discharge port of the second spray section 12. The absorbent discharged from the second spray section 12 can be stored in the phase separator 9. In the phase separator 9, due to the different densities of the lean liquid and the rich liquid, the rich liquid is collected at the bottom of the phase separator 9, while the lean liquid is located on the upper layer of the rich liquid. The lean liquid and the rich liquid can be extracted separately by using a pump. Among them, the extracted lean liquid can be passed into the second spray section 12 to react with the flue gas again, and the extracted rich liquid is passed into the regeneration tower 2 for regeneration after passing through the preheating heat exchanger 7.

[0053] It can be understood that the use of the phase separator 9 to separate the rich and lean liquids of the absorbent in the second spray section 12 ensures the circulation of the absorbent in the second spray pipeline 82 and facilitates the preheating and regeneration of the rich liquid.

[0054] In some embodiments, a cooler 84 is provided on the third spray pipeline 83, and the cooling outlet of the absorption refrigerator 5 is connected to the cooler 84. Figure 1 As shown, the third spray pipeline 83 is connected to the cooler 84, so that the cooler 84 can cool the third spray pipeline 83, thereby reducing the temperature of the absorbent in the third spray pipeline 83.

[0055] That is to say, after the absorbent in the third spray section 13 reacts with the flue gas, the temperature of the absorbent increases, which reduces its effect of removing pollutants in the flue gas. Therefore, the cooler 84 is used to cool the absorbent in the third spray pipeline 83, which ensures the removal effect of the absorbent and avoids energy waste.

[0056] In some embodiments, the third spray pipeline 83 has an absorbent discharge port 831, and the absorbent discharge port 831 is connected to the regeneration tower 2. It can be understood that if Figure 1As shown, after the absorbent in the third spray section 13 reacts with the flue gas, the lean liquid will gradually turn into rich liquid. The rich liquid in the third spray section 13 is extracted by the third spray pipeline 83 and passed into the regeneration tower 2 through the absorbent discharge port 831 to regenerate the absorbent.

[0057] In some embodiments, the separator 3 has a regeneration gas inlet 31, the regeneration gas outlet of the regeneration tower 2 is connected to the regeneration gas inlet 31, and the cooling outlet of the absorption refrigerator 5 is connected to the regeneration gas inlet 31. It can be understood that Figure 1 As shown, the third spray pipeline 83 passes the rich liquid in the third spray section 13 into the regeneration tower 2 for regeneration, and the total amount of absorbent in the third spray section 13 is reduced, which affects the reaction between the absorbent and the flue gas. Therefore, the absorbent separated in the separator 3 is passed into the third spray section 13 to maintain sufficient absorbent in the third spray section 13 for reaction with the flue gas.

[0058] In addition, the regeneration gas discharged from the regeneration tower 2 still has a certain temperature. Using the cold discharged from the cooling outlet of the absorption refrigerator 5 to cool this part of the regeneration gas is beneficial to the separation of the regeneration gas in the separator 3, and further improves the separation effect of the regeneration gas and the absorbent.

[0059] In some embodiments, the flue gas carbon dioxide capture and storage system of the embodiment of the present invention also includes a regeneration water cooler 10, the hot side inlet of the regeneration water cooler 10 is connected to the regeneration gas outlet of the regeneration tower 2, the hot side outlet of the regeneration water cooler 10 is connected to the regeneration gas inlet 31, and the cold side inlet of the regeneration water cooler 10 is connected to the cooling outlet of the absorption chiller 5.

[0060] It is understandable that if Figure 1 As shown, the cold discharged from the cooling outlet of the absorption refrigerator 5 can cool the cooling medium in the regeneration water cooler 10, so that the cooled cooling medium can exchange heat with the regeneration gas, thereby avoiding the cold discharged from the cooling outlet of the absorption refrigerator 5 from directly mixing with the regeneration gas, thereby avoiding the mixing of other impurity gases in the regeneration gas, which is beneficial to the separation of the regeneration gas.

[0061] In some embodiments, the separator 3 also has a separation liquid outlet 32, and the third spray pipeline 83 also has an absorbent inlet 832, the absorbent inlet 832 is located downstream of the absorbent discharge port 831, and the absorbent inlet 832 is located upstream of the cooler 84, and the separation liquid outlet 32 ​​is connected to the absorbent inlet 832.

[0062] It is understandable that if Figure 1As shown, the absorbent discharged from the separation liquid outlet 32 ​​can be passed into the third spray pipeline 83 to be used for re-spraying the third spray section 13. The absorbent inlet 832 is located upstream of the cooler 84, so that the absorbent discharged from the separation liquid outlet 32 ​​is mixed with the absorbent in the third spray pipeline 83 and then cooled by the cooler 84, thereby ensuring the overall concentration and temperature of the absorbent, thereby improving the reaction effect of the absorbent and the flue gas.

[0063] In some embodiments, the third spray pipeline 83 is further provided with a mixer 85, and the mixer 85 is connected to the separation liquid outlet 32. It can be understood that if Figure 1 As shown, the absorbent liquid inlet 832 is arranged on the mixer 85, and the absorbent discharged from the separation liquid outlet 32 ​​and the absorbent in the third spray pipeline 83 can be fully mixed in the mixer 85 to ensure the solution concentration of the absorbent, which is conducive to the reaction between the absorbent and the flue gas.

[0064] In the description of the present invention, it is to be understood that the terms “center”, “longitudinal”, “lateral”, “length”, “width”, “thickness”, “up”, “down”, “front”, “back”, “left”, “right”, “vertical”, “horizontal”, “top”, “bottom”, “inside”, “outside”, “clockwise”, “counterclockwise”, “axial”, “radial”, “circumferential”, etc., indicating orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0065] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0066] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral one; it can be a mechanical connection, an electrical connection, or communication with each other; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0067] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0068] In the present invention, the terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" etc. mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the described specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0069] Although the above embodiments have been shown and described, it is to be understood that the above embodiments are exemplary and are not to be construed as limitations on the present invention. Changes, modifications, substitutions and variations of the above embodiments by those of ordinary skill in the art are all within the scope of protection of the present invention.

Claims

1. A flue gas carbon dioxide capture and storage system, characterized in that: include: An absorption tower, wherein the absorption tower has a flue gas inlet, and the flue gas inlet is used to introduce the pretreated flue gas; A regeneration tower, the regeneration tower is connected to the absorption tower, the absorbent in the absorption tower reacts with the flue gas to form a saturated absorbent and is passed into the regeneration tower, the regeneration tower is used to desorb the saturated absorbent and then pass it into the absorption tower; A separator, the separator is connected to the regeneration tower so that the regeneration gas discharged from the regeneration tower is separated into gas and liquid in the separator; A sealing unit, the sealing unit comprising a compression component and a drying component, the compression component is connected to the separator to compress the gas discharged from the separator, and the drying component is connected to the compression component to dry part of the gas in the compression component, The drying assembly includes a drying tower and a heater, wherein the heater is connected to the drying tower to heat the desiccant discharged from the drying tower and then pass the desiccant into the drying tower after being heated; An absorption refrigerator, wherein a hot side inlet of the absorption refrigerator is connected to a vapor outlet of the heater, and a cold side outlet of the absorption refrigerator is connected to at least one of the separator and the absorption tower.

2. The flue gas carbon dioxide capture and storage system according to claim 1, characterized in that: It also includes a lean-rich liquid heat exchanger, which is connected to both the absorption tower and the regeneration tower, so that the saturated absorbent discharged from the absorption tower and the desorbed absorbent discharged from the regeneration tower can exchange heat, and the desorbed absorbent is used to pass into the absorption tower, and the saturated absorbent is used to pass into the regeneration tower.

3. The flue gas carbon dioxide capture and storage system according to claim 2, characterized in that: It also includes a preheating heat exchanger, and the absorber includes a first spray section, a second spray section and a third spray section arranged in sequence along the direction of flue gas flow, the first spray section, the second spray section and the third spray section are respectively connected to a first spray pipeline, a second spray pipeline and a third spray pipeline, the second spray pipeline has a rich liquid outlet, and the rich liquid outlet is connected to the lean-rich liquid heat exchanger through a rich liquid pipeline, and the preheating heat exchanger is connected to the first spray pipeline and the rich liquid pipeline, so that the rich liquid pipeline and the first spray pipeline exchange heat in the preheating heat exchanger.

4. The flue gas carbon dioxide capture and storage system according to claim 3, characterized in that: It also includes a phase separator, which has a phase separation inlet, a first phase separation outlet and a second phase separation outlet, the phase separation inlet is connected to the rich liquid outlet, the first phase separation outlet is connected to the spray inlet of the second spray section, and the second phase separation outlet is connected to the rich liquid pipeline.

5. The flue gas carbon dioxide capture and storage system according to claim 3, characterized in that: The third spray pipeline is provided with a cooler, and the cooling outlet of the absorption refrigerator is connected to the cooler.

6. The flue gas carbon dioxide capture and storage system according to claim 5, characterized in that: The third spray pipeline has an absorbent liquid discharge port, and the absorbent liquid discharge port is connected to the regeneration tower.

7. The flue gas carbon dioxide capture and storage system according to claim 6, characterized in that: The separator has a regeneration gas inlet, the regeneration gas outlet of the regeneration tower is connected to the regeneration gas inlet, and the cooling outlet of the absorption refrigerator is connected to the regeneration gas inlet.

8. The flue gas carbon dioxide capture and storage system according to claim 7, characterized in that: It also includes a regenerative water cooler, wherein the hot side inlet of the regenerative water cooler is connected to the regeneration gas outlet of the regeneration tower, the hot side outlet of the regenerative water cooler is connected to the regeneration gas inlet, and the cold side inlet of the regenerative water cooler is connected to the cooling outlet of the absorption refrigerator.

9. The flue gas carbon dioxide capture and storage system according to claim 8, characterized in that: The separator also has a separation liquid outlet, and the third spray pipeline also has an absorbent inlet, which is located downstream of the absorbent discharge port and upstream of the cooler, and the separation liquid outlet is connected to the absorbent inlet.

10. The flue gas carbon dioxide capture and storage system according to claim 9, characterized in that: The third spray pipeline is also provided with a mixer, and the mixer is connected to the separation liquid outlet.

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