CN219539893U - Carbon dioxide trapping system and carbon dioxide treatment system - Google Patents
Carbon dioxide trapping system and carbon dioxide treatment system Download PDFInfo
- Publication number
- CN219539893U CN219539893U CN202320948879.7U CN202320948879U CN219539893U CN 219539893 U CN219539893 U CN 219539893U CN 202320948879 U CN202320948879 U CN 202320948879U CN 219539893 U CN219539893 U CN 219539893U
- Authority
- CN
- China
- Prior art keywords
- rich
- inlet
- lean
- carbon dioxide
- rich liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a carbon dioxide capturing system and a carbon dioxide processing system, wherein the system comprises an absorption tower, a desorption tower, a lean-rich liquid heat exchanger, a rich liquid reheater, a reboiler and a reflux tank; the rich liquor outlet of the absorption tower is connected with the rich liquor inlet of the lean and rich liquor heat exchanger, and the rich liquor outlet of the lean and rich liquor heat exchanger is respectively connected with the rich liquor inlet of the rich liquor reheater and the first rich liquor inlet of the desorption tower; the rich liquid outlet of the rich liquid reheating device is connected with the second rich liquid inlet of the desorption tower; the steam condensate outlet of the reboiler is connected with the steam condensate inlet of the rich liquid reheating device; the rich liquid reheater is suitable for transferring the heat of the absorbed steam condensate from the reboiler to the rich liquid from the absorption tower; a tower bottom liquid outlet of the desorption tower is connected with a tower bottom liquid inlet of the reboiler; the gas outlet of the reboiler is connected with the gas inlet of the desorption tower; the gas outlet of the desorption tower is connected with the inlet of the reflux tank; the system fully utilizes waste heat resources and saves steam consumption of the reboiler.
Description
Technical Field
The utility model relates to the technical field of carbon capture, in particular to a carbon dioxide capture system and a carbon dioxide treatment system.
Background
With the increase of the greenhouse effect of carbon dioxide, carbon capture and sequestration (CCUS) technology is becoming more and more important worldwide. The paris protocol strives to control the temperature control target within 1.5 ℃, and the global carbon dioxide emission reduction must reach more than 80% by 2050, so carbon capture and sequestration (CCUS) technology becomes a necessary technical means for achieving the dual carbon target.
Among the existing carbon trapping technologies, the carbon dioxide trapping technology using an organic composite alcohol amine solution as a chemical absorbent is a main technology which can be applied to large-scale industrialization at present, and the technology uses an alkaline alcohol amine solution as a solvent to absorb and desorb CO in flue gas through two processes 2 And (5) collecting and purifying. In the absorption and desorption process, after the high Wen Pinye at the bottom of the desorption tower exchanges heat with the rich liquid from the bottom of the absorption tower through a lean-rich liquid heat exchanger, the lean liquid is cooled and sent to a lean liquid cooler to be continuously cooled to a proper temperature to enter the absorption tower, and the rich liquid is heated and enters the desorption tower to carry out desorption reaction, and whether the heat exchange optimization scheme in the process reasonably directly influences the whole energy consumption of trapping or not.
Disclosure of Invention
In order to enrich the types of carbon capture systems and increase the selection space of energy-saving modes in the carbon capture process, the utility model provides a carbon dioxide capture system and a carbon dioxide treatment system.
In a first aspect, an embodiment of the present utility model provides a carbon dioxide capturing system, including an absorption tower, a desorption tower, a lean-rich liquid heat exchanger, a rich liquid reheater, a reboiler, and a reflux tank;
the rich liquor outlet of the absorption tower is connected with the rich liquor inlet of the lean and rich liquor heat exchanger, and the rich liquor outlet of the lean and rich liquor heat exchanger is respectively connected with the rich liquor inlet of the rich liquor reheater and the first rich liquor inlet of the desorption tower; the rich liquid outlet of the rich liquid reheating device is connected with the second rich liquid inlet of the desorption tower;
the steam condensate outlet of the reboiler is connected with the steam condensate inlet of the rich liquid reheater; the rich liquid reheater is suitable for transferring the absorbed heat of the steam condensate from the reboiler to the rich liquid from the absorption tower;
the lean solution outlet of the reboiler is connected with the lean solution inlet of the lean-rich solution heat exchanger, and the lean solution outlet of the lean-rich solution heat exchanger is connected with the lean solution inlet of the absorption tower;
the tower bottom liquid outlet of the desorption tower is connected with the tower bottom liquid inlet of the reboiler; the gas outlet of the reboiler is connected with the gas inlet of the desorption tower; the gas outlet of the desorption tower is connected with the inlet of the reflux tank; and a condensate outlet of the reflux tank is connected with a condensate inlet of the desorption tower.
In one or some alternative embodiments, the first rich liquid inlet of the desorber is disposed at the top of the desorber;
the second rich liquid inlet of the desorption tower is arranged at the bottom of the desorption tower.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a lean liquor cooler;
and the lean solution cooler is respectively connected with a lean solution outlet of the lean-rich solution heat exchanger and a lean solution inlet of the absorption tower.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a regeneration gas cooler;
the regenerated gas cooler is respectively connected with the gas outlet of the desorption tower and the inlet of the reflux tank.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a rich liquid transfer pump;
the rich liquid delivery pump is arranged between a rich liquid outlet of the absorption tower and a rich liquid inlet of the lean rich liquid heat exchanger.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a lean solution transfer pump;
the lean solution delivery pump is arranged between a lean solution outlet of the reboiler and a lean solution inlet of the lean-rich solution heat exchanger.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a reflux pump;
the reflux pump is arranged between the condensate outlet of the reflux tank and the condensate inlet of the desorption tower.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a steam supply device;
the steam supply device is connected with a steam inlet of the reboiler and is used for supplying steam to the reboiler;
in one or some alternative embodiments, the carbon dioxide capture system further comprises a vapor condensate recovery device;
the steam condensate recovery device is connected with the steam condensate outlet of the rich liquor reheater and is used for recovering the steam condensate discharged from the rich liquor reheater.
In one or some alternative embodiments, the carbon dioxide capture system further comprises a flue gas pretreatment device coupled to the absorber tower.
In a second aspect, an embodiment of the present utility model provides a carbon dioxide treatment system, including a carbon dioxide treatment unit and the carbon dioxide capturing system connected to the carbon dioxide treatment unit.
The technical scheme provided by the embodiment of the utility model has the beneficial effects that at least:
according to the carbon dioxide trapping system provided by the embodiment, after the rich liquid from the absorption tower is subjected to heat exchange and temperature rise through the lean-rich liquid heat exchanger, the rich liquid is split into two branches which respectively flow to different positions of the desorption tower, compared with the direct split of the low-temperature rich liquid from the absorption tower, the rich liquid passing through the lean-rich liquid heat exchanger is more, the rich liquid exchanges heat with the lean liquid in the lean-rich liquid heat exchanger more fully, the problem that the rich liquid temperature rise cannot be improved due to end difference limitation of the lean-rich liquid heat exchanger is solved, and the heat quantity of the lean liquid absorbed by the rich liquid is more, so that the energy consumption required for cooling the lean liquid is reduced. After the rich liquid enters the desorption tower after heat exchange and temperature rise, heat is provided for desorption reaction besides desorption, and steam consumption of a reboiler is reduced. Through setting up the rich liquor reheater to the steam condensate that produces in the reboiler lets in the rich liquor reheater, utilizes the heat of steam condensate to carry out the secondary heating to the rich liquor that passes through the rich liquor reheater and intensifies, and the rich liquor after the secondary heating intensifies gets into the bottom of desorber and provides the heat for desorption reaction, has fully utilized waste heat resource, simultaneously, is used for heating the rich liquor with the steam condensate, has saved the steam consumption of reboiler.
Additional features and advantages of the utility model will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the utility model. The objectives and other advantages of the utility model may be realized and attained by the structure particularly pointed out in the written description and drawings.
The technical scheme of the utility model is further described in detail through the drawings and the embodiments.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate the utility model and together with the embodiments of the utility model, serve to explain the utility model. In the drawings:
FIG. 1 is a schematic diagram of a carbon dioxide capture system according to an embodiment of the present utility model;
fig. 2 is a schematic structural diagram of a carbon dioxide treatment system according to an embodiment of the present utility model.
In the figure:
the device comprises an absorption tower 1, a desorption tower 2, a lean-rich liquid heat exchanger 3, a rich liquid reheater 4, a reboiler 5, a reflux tank 6, a lean liquid cooler 7, a regenerated gas cooler 8, a rich liquid delivery pump 9, a lean liquid delivery pump 10, a reflux pump 11, a steam supply device 12, a steam condensate recovery device 13 and a flue gas pretreatment device 14;
100 is a carbon dioxide capture system and 200 is a carbon dioxide treatment unit.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art.
In the description of the present utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," "outer," "far," "near," "front," "rear," and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, merely to facilitate description of the present utility model and simplify the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
The inventor finds that the CO in the flue gas can be recovered by the composite alcohol amine capturing technology 2 The trapping is performed, but the trapping energy consumption is high, so that the wide application is difficult. In the composite alcohol amine trapping technology, CO is absorbed 2 The energy consumption of desorption and regeneration of the rich liquid after the process is about 60% of the energy consumption of the whole trapping process, and the method has great practical significance in effectively reducing the energy consumption of desorption and regeneration of the rich liquid.
The existing rich liquid diversion technology is that the rich liquid at the bottom of the absorption tower is divided into two parts, one part is heated by a lean and rich liquid heat exchanger and then enters the desorption tower, and the other part is directly enters the top of the desorption tower without being heated by the lean and rich liquid heat exchanger, and in the process, the amount of the rich liquid passing through the lean and rich liquid heat exchanger is reduced, so that the temperature rise of the rich liquid is increased. However, in engineering practice, the lean-rich liquid heat exchanger has end difference limitation, so that the rich liquid temperature rise cannot be improved, and the effect of reducing the steam consumption cannot be achieved; on the other hand, the flow of the rich liquid passing through the lean-rich liquid heat exchanger is reduced, so that the temperature of the lean liquid passing through the lean-rich liquid heat exchanger is increased, namely the heat transferred to the rich liquid by the lean liquid is reduced, and finally the cooling capacity is increased to cool the lean liquid, so that the energy-saving effect is not obvious as a whole.
Based on this, the embodiment of the present utility model provides a carbon dioxide capturing system and a carbon dioxide processing system, and the following description will explain by specific embodiments.
Example 1
The present embodiment provides a carbon dioxide capturing system 100, which is shown with reference to fig. 1, including an absorption tower 1, a desorption tower 2, a lean-rich liquid heat exchanger 3, a rich liquid reheater 4, a reboiler 5, and a reflux drum 6;
the rich liquor outlet of the absorption tower 1 is connected with the rich liquor inlet of the lean rich liquor heat exchanger 3, and the rich liquor outlet of the lean rich liquor heat exchanger 3 is respectively connected with the rich liquor inlet of the rich liquor reheater 4 and the first rich liquor inlet of the desorption tower 2; the rich liquor outlet of the rich liquor reheater 4 is connected with the second rich liquor inlet of the desorption tower 2;
the steam condensate outlet of the reboiler 5 is connected with the steam condensate inlet of the rich liquor reheater 4; the rich liquid reheater 4 is adapted to transfer the heat of the absorbed steam condensate from the reboiler 5 to the rich liquid from the absorber 1;
the lean solution outlet of the reboiler 5 is connected with the lean solution inlet of the lean-rich solution heat exchanger 3, and the lean solution outlet of the lean-rich solution heat exchanger 3 is connected with the lean solution inlet of the absorption tower 1;
the tower bottom liquid outlet of the desorption tower 2 is connected with the tower bottom liquid inlet of the reboiler 5; the gas outlet of the reboiler 5 is connected with the gas inlet of the desorption tower 2; the gas outlet of the desorption tower 2 is connected with the inlet of the reflux tank 6; the condensate outlet of the reflux tank 6 is connected with the condensate inlet of the desorption tower 2.
In the present embodiment, the lean solution is capable of reacting with CO 2 The absorbent in which the decarburization reaction occurs may be, for example, an ethanolamine solution; containing CO 2 The flue gas enters the absorption tower 1 after impurity removal and temperature reduction, and lean solution sprays the flue gas from top to bottom in the absorption tower 1 to mix with CO in the flue gas 2 Decarburization reaction is carried out to CO 2 Absorbing. Lean liquid absorbing CO 2 And then becomes a rich liquid, which flows out from the absorption tower 1 and then flows to the desorption tower 2 for desorption.
In this embodiment, the rich liquid outlet of the absorption tower 1 is disposed at the bottom of the absorption tower 1, the rich liquid coming out from the bottom of the absorption tower 1 firstly enters the lean rich liquid heat exchanger 3 to exchange heat and raise the temperature to 90-100 ℃, the rich liquid after temperature rise is divided into two parts, one part enters the desorption tower 2 to desorb, the other part enters the rich liquid reheater 4 to further heat and raise the temperature to 105-120 ℃, and the rich liquid after secondary temperature rise enters the desorption tower 2 to desorb. The rich liquid from the lean-rich liquid heat exchanger 3 which does not pass through the rich liquid reheating heater 4 enters the desorption tower 2 through the first rich liquid inlet of the desorption tower 2 to be desorbed, and meanwhile, the temperature of the regenerated gas at the top of the desorption tower 2 is reduced, so that the content of water vapor in the tower top gas is reduced. The rich liquid which is secondarily warmed up by the rich liquid reheater 4 enters the desorption tower 2 through a second rich liquid inlet of the desorption tower 2 to be desorbed, and simultaneously, heat is provided for desorption reaction in the desorption tower 2 at the bottom of the desorption tower 2.
In this embodiment, the first rich liquid inlet of the desorption tower 2 is disposed at the top of the desorption tower 2, and the second rich liquid inlet of the desorption tower 2 is disposed at the bottom of the desorption tower 2. Since the desorption reaction in the desorption tower 2 requires heat and the temperature in the desorption tower 2 increases downward, in order to prevent heat loss in the rich liquid after the secondary temperature rise and the temperature rise of the regeneration gas, the rich liquid after the secondary temperature rise by the rich liquid reheater 4 enters the trays in the lower part of the desorption tower 2 from the second rich liquid inlet of the desorption tower 2, specifically, the trays 1 to 5 from bottom to top in the desorption tower 2.
In the carbon dioxide capturing system 100 provided in this embodiment, after the rich liquid from the absorption tower 1 is subjected to heat exchange and temperature rise by the lean-rich liquid heat exchanger 3, the rich liquid is split into two branches which respectively flow to different positions of the desorption tower 2, compared with the direct split of the low-temperature rich liquid from the absorption tower 1, the rich liquid passing through the lean-rich liquid heat exchanger 3 is more, the rich liquid exchanges heat with the lean liquid in the lean-rich liquid heat exchanger 3 more fully, the problem that the rich liquid temperature rise caused by end difference limitation of the lean-rich liquid heat exchanger 3 cannot be improved is solved, and the heat quantity of the lean liquid absorbed by the rich liquid is more, so that the energy consumption required for cooling the lean liquid is reduced. After the rich liquid enters the desorption tower 2 after heat exchange and temperature rise, heat is provided for desorption reaction besides desorption, and steam consumption of the reboiler 5 is reduced.
In this embodiment, after the rich liquid enters the desorption tower 2 for desorption, the regenerated gas is decomposed, and the main component in the regenerated gas is CO 2 And water vapor; the rich liquid is decomposed to form regenerated gas, and then is converted into lean liquid, and the lean liquid can flow to the absorption tower 1 for the next round of absorption.
The carbon dioxide capturing system 100 provided in this embodiment further includes a steam supply device 12, where the steam supply device 12 is connected to the steam inlet of the reboiler 5, and is used for providing steam to the reboiler 5. The reboiler 5 may be disposed at the side or lower part of the bottom of the desorption tower 2, two rich liquids from the lean-rich liquid heat exchanger 3 respectively enter the desorption tower 2 from the first rich liquid inlet and the second rich liquid inlet of the desorption tower 2 for desorption, the bottom liquid of the desorption tower 2 enters the reboiler 5 for flash evaporation, and the flash evaporation is performed to obtain CO-containing liquid 2 The flash gas is continuously risen after returning to the desorption tower 2, and contacts with the downward flowing rich liquid in the desorption tower 2 in the rising process, thereby carrying out CO 2 Desorbing; the remaining liquid in the reboiler 5 is sent to the lean/rich liquid heat exchanger 3, exchanges heat with the rich liquid passing through the lean/rich liquid heat exchanger 3, and is then sent to the absorption column 1. During desorption, the heat of reboiler 5The steam from the steam supply 12 may be low pressure steam at a pressure of 0.3 MPaG.
In this embodiment, heat of steam introduced into the reboiler 5 is absorbed and converted into steam condensate, and a steam condensate outlet of the reboiler 5 is connected to a steam condensate inlet of the rich liquor reheater 4. The reboiler 5 provides heat for the desorption reaction in the desorption tower 2, the heat supply process only uses the phase change latent heat of the steam, the temperature of the steam condensate flowing out of the reboiler 5 is still the saturation temperature of the steam under the pressure at that time, and the temperature difference between the steam condensate and the rich liquid passing through the lean-rich liquid heat exchanger 3 is still about 40 ℃. Therefore, the steam condensate is sent to the rich liquid reheater 4 to exchange heat with the rich liquid heated by heat exchange, and the rich liquid is heated to about 105 to 120 ℃ and then sent to the desorption tower 2. If the high Wen Fuye after the secondary temperature rise enters from the upper part of the desorption tower 2, the temperature of the regenerated gas at the top of the desorption tower 2 is increased, which is unfavorable for energy conservation, so that the high-temperature rich liquid after the secondary temperature rise is sent to the bottom of the desorption tower 2 for desorption, heat is provided for desorption reaction, and the steam consumption of the reboiler 5 is reduced.
The carbon dioxide capturing system 100 provided in this embodiment further includes a steam condensate recovery apparatus 13; the steam condensate recovery device 13 is connected to a steam condensate outlet of the rich liquor reheater 4 and is used for recovering steam condensate discharged from the rich liquor reheater 4.
In a specific embodiment, the heat source of the rich liquid reheater 4 may be steam condensate of the tower kettle reboiler 5, or may utilize the existing rich low-temperature heat source in the factory, so as to facilitate the energy optimization in the whole factory, and achieve the effects of energy conservation and emission reduction.
According to the carbon dioxide capturing system 100 provided by the embodiment, the rich liquid reheater 4 is arranged, the steam condensate generated in the reboiler 5 is led into the rich liquid reheater 4, the heat of the steam condensate is utilized to carry out secondary heating and temperature rising on the rich liquid passing through the rich liquid reheater 4, the rich liquid after the secondary heating and temperature rising enters the bottom of the desorption tower 2 to provide heat for desorption reaction, waste heat resources are fully utilized, and meanwhile, the steam condensate is used for heating the rich liquid, so that the burden of treating the steam condensate is reduced, and the steam consumption of the reboiler 5 is saved.
In a specific embodiment, referring to fig. 1, the carbon dioxide capturing system 100 further includes a lean solution cooler 7 disposed between the lean solution outlet of the lean rich solution heat exchanger 3 and the lean solution inlet of the absorption tower 1; the lean solution from the rich solution heat exchanger flows to the absorption tower 1 after being cooled by the lean solution cooler 7, sprays the flue gas from top to bottom in the absorption tower 1, and absorbs CO in the flue gas 2 。
In a specific embodiment, referring to fig. 1, the carbon dioxide capture system 100 further comprises a regeneration gas cooler 8 disposed between the gas outlet of the desorber 2 and the inlet of the reflux drum 6; the desorption reaction takes place in the desorption tower 2 to obtain regenerated gas, the regenerated gas from the top of the desorption tower 2 is cooled by a regenerated gas cooler 8 and flows to a reflux tank 6, and is separated into CO in the reflux tank 6 2 And condensed water, which flows out from the reflux drum 6, returns to the desorption tower 2 through the condensate inlet of the desorption tower 2, and is CO 2 To an external carbon dioxide processing unit 200.
In a specific embodiment, referring to fig. 1, the carbon dioxide capturing system 100 further includes a rich liquid transfer pump 9 disposed between the rich liquid outlet of the absorption tower 1 and the rich liquid inlet of the lean rich liquid heat exchanger 3; the rich liquid outlet of the absorption tower 1 is arranged at the bottom of the absorption tower 1, and the rich liquid flowing out of the bottom of the absorption tower 1 can be pumped into the lean-rich liquid heat exchanger 3 through the rich liquid delivery pump 9.
In a specific embodiment, referring to fig. 1, the carbon dioxide capturing system 100 further includes a lean solution transfer pump 10 disposed between the lean solution outlet of the reboiler 5 and the lean solution inlet of the lean-rich solution heat exchanger 3; the lean liquid outlet of the reboiler 5 is arranged at the bottom of the reboiler 5, and the lean liquid in the reboiler 5 can be pumped into the lean-rich liquid heat exchanger 3 by the lean liquid delivery pump 10.
In one embodiment, referring to fig. 1, the carbon dioxide capturing system 100 further includes a reflux pump 11 disposed between the condensate outlet of the reflux drum 6 and the condensate inlet of the desorption tower 2; the vapor condensate in the reflux drum 6 can be pumped into the desorption column 2 by the reflux pump 11 and flows downward in the desorption column 2.
In one embodiment, referring to FIG. 1, the carbon dioxide capture system 100 further comprises a flue gas pretreatment device 14 coupled to the absorber tower 1; the flue gas is subjected to impurity removal and temperature reduction in the flue gas pretreatment device 14, and then is introduced into the absorption tower 1 for decarburization treatment.
The carbon dioxide capturing system 100 provided in this embodiment is used for capturing carbon dioxide, and a specific process flow may include:
after the flue gas is subjected to impurity removal and cooling treatment by the flue gas pretreatment device 14, the flue gas is introduced into the absorption tower 1 from a flue gas inlet at the bottom of the absorption tower 1, lean solution is sprayed downwards from a lean solution inlet at the top of the absorption tower 11, and CO in the flue gas 2 Countercurrent contact with lean solution, decarburization reaction occurs, and decarburization gas flows through an absorption section and a tail gas washing section of the absorption tower 11 in sequence and is discharged from the top of the tower; lean liquid for absorbing CO in flue gas 2 Then, the mixture becomes rich liquid;
the rich liquid is discharged from the bottom of the absorption tower 11, is heated to 90-100 ℃ through heat exchange of the lean-rich liquid heat exchanger 3, is divided into two streams, and one stream directly enters the desorption tower 2 through a first rich liquid inlet of the desorption tower 2, flows from top to bottom in the desorption tower 2 under the action of gravity, and CO in the rich liquid flows in the flowing process 2 The reaction product is heated and decomposed in the tower to obtain regenerated gas, the regenerated gas is discharged from the top of the desorption tower 2 and respectively passes through a regenerated gas cooler 8 and a reflux tank 6, and the CO obtained after condensation and separation is obtained 2 To the carbon dioxide treatment unit 200, the condensed water is sent back to the desorption tower 2; and the other stock of rich liquid enters a rich liquid reheating device 4 for secondary heating, enters a desorption tower 2 from a second rich liquid inlet of the desorption tower 2 for desorption, and provides heat for desorption reaction.
The heat required by the desorption process is provided by the rich liquid and the reboiler 5 after temperature rise, and the heat of the reboiler 5 is derived from low-pressure steam provided by the steam supply device 12; the steam condensate coming out of the reboiler 5 is subjected to heat exchange by the condensate-removing reheater 4, and then is sent to the steam condensate recovery apparatus 13.
The lean solution discharged from the bottom of the desorption tower 2 is sent to the lean-rich solution heat exchanger 3 through the lean solution delivery pump 10, fully exchanges heat with the rich solution from the bottom of the absorption tower 1, enters the lean solution cooler 7 for further cooling after the temperature is reduced to a first preset temperature value, and enters the top of the absorption tower 1 for cyclic absorption after the temperature of the lean solution is cooled to a second preset temperature value.
According to the carbon dioxide capturing system 100 provided by the embodiment, according to the characteristics of the carbon dioxide absorbent, the limit of the end difference of the lean and rich liquid heat exchanger 3 and the feasibility of engineering implementation, the rich liquid diversion position is arranged on the lean and rich liquid heat exchanger 3, so that the lean liquid and the rich liquid exchange heat more fully, and the rich liquid after heat exchange enters the desorption tower 2 to provide heat for the desorption reaction, so that the steam consumption of the reboiler 5 is reduced; the steam condensate generated in the reboiler 5 is led into the rich liquor reheater 4, and the heat of the steam condensate is transferred to the rich liquor through the rich liquor reheater 4, so that the rich liquor is heated for the second time, the utilization rate of the residual heat is improved, the steam consumption is reduced, and the running cost and the energy consumption of carbon capture are effectively reduced.
The inventors found that, taking the MEA system as an example, the carbon dioxide capturing system 100 provided with the rich liquid reheater 4 can reduce the steam consumption by about 3% to 5% by comparing the steam consumed in the carbon capturing process with the carbon dioxide capturing system 100 provided with the rich liquid reheater 4, under the other conditions the same.
Example two
Based on the same inventive concept, the present embodiment provides a carbon dioxide treatment system including a carbon dioxide treatment unit 200 and the carbon dioxide capture system 100 described in the above embodiment one connected to the carbon dioxide treatment unit 200. The reflux drum 6 of the carbon dioxide capturing system 100 is connected to the carbon dioxide processing unit 200, and CO discharged from the reflux drum 6 2 Enters the carbon dioxide processing unit 200 for compression, liquefaction and storage.
It will be apparent to those skilled in the art that various modifications and variations can be made to the present utility model without departing from the spirit or scope of the utility model. The present disclosure is not limited to the precise construction that has been described above and shown in the drawings, and various modifications and changes may be made without departing from the scope thereof. The scope of the present disclosure is limited only by the appended claims. Thus, it is intended that the present utility model also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof.
Claims (11)
1. The carbon dioxide capturing system is characterized by comprising an absorption tower, a desorption tower, a lean-rich liquid heat exchanger, a rich liquid reheater, a reboiler and a reflux tank;
the rich liquor outlet of the absorption tower is connected with the rich liquor inlet of the lean and rich liquor heat exchanger, and the rich liquor outlet of the lean and rich liquor heat exchanger is respectively connected with the rich liquor inlet of the rich liquor reheater and the first rich liquor inlet of the desorption tower; the rich liquid outlet of the rich liquid reheating device is connected with the second rich liquid inlet of the desorption tower;
the steam condensate outlet of the reboiler is connected with the steam condensate inlet of the rich liquid reheater; the rich liquid reheater is suitable for transferring the absorbed heat of the steam condensate from the reboiler to the rich liquid from the absorption tower;
the lean solution outlet of the reboiler is connected with the lean solution inlet of the lean-rich solution heat exchanger, and the lean solution outlet of the lean-rich solution heat exchanger is connected with the lean solution inlet of the absorption tower;
the tower bottom liquid outlet of the desorption tower is connected with the tower bottom liquid inlet of the reboiler; the gas outlet of the reboiler is connected with the gas inlet of the desorption tower; the gas outlet of the desorption tower is connected with the inlet of the reflux tank; and a condensate outlet of the reflux tank is connected with a condensate inlet of the desorption tower.
2. The carbon dioxide capture system of claim 1, wherein the first rich liquid inlet of the desorber is disposed at a top of the desorber;
the second rich liquid inlet of the desorption tower is arranged at the bottom of the desorption tower.
3. The carbon dioxide capture system of claim 1, further comprising a lean liquor cooler;
and the lean solution cooler is respectively connected with a lean solution outlet of the lean-rich solution heat exchanger and a lean solution inlet of the absorption tower.
4. The carbon dioxide capture system of claim 1, further comprising a regeneration gas cooler;
the regenerated gas cooler is respectively connected with the gas outlet of the desorption tower and the inlet of the reflux tank.
5. The carbon dioxide capture system of claim 1, further comprising a rich liquor transfer pump;
the rich liquid delivery pump is arranged between a rich liquid outlet of the absorption tower and a rich liquid inlet of the lean rich liquid heat exchanger.
6. The carbon dioxide capture system of claim 1, further comprising a lean solution transfer pump;
the lean solution delivery pump is arranged between a lean solution outlet of the reboiler and a lean solution inlet of the lean-rich solution heat exchanger.
7. The carbon dioxide capture system of claim 1, further comprising a return pump;
the reflux pump is arranged between the condensate outlet of the reflux tank and the condensate inlet of the desorption tower.
8. The carbon dioxide capture system of claim 1, further comprising a steam supply device;
the steam supply device is connected with a steam inlet of the reboiler and is used for supplying steam to the reboiler.
9. The carbon dioxide capture system of claim 1, further comprising a steam condensate recovery device;
the steam condensate recovery device is connected with the steam condensate outlet of the rich liquor reheater and is used for recovering the steam condensate discharged from the rich liquor reheater.
10. The carbon dioxide capture system of claim 1, further comprising a flue gas pretreatment device coupled to the absorber tower.
11. A carbon dioxide treatment system comprising a carbon dioxide treatment unit and a carbon dioxide capture system according to any one of claims 1 to 9 connected to the carbon dioxide treatment unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320948879.7U CN219539893U (en) | 2023-04-24 | 2023-04-24 | Carbon dioxide trapping system and carbon dioxide treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320948879.7U CN219539893U (en) | 2023-04-24 | 2023-04-24 | Carbon dioxide trapping system and carbon dioxide treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219539893U true CN219539893U (en) | 2023-08-18 |
Family
ID=87736688
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320948879.7U Active CN219539893U (en) | 2023-04-24 | 2023-04-24 | Carbon dioxide trapping system and carbon dioxide treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219539893U (en) |
-
2023
- 2023-04-24 CN CN202320948879.7U patent/CN219539893U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103619443B (en) | The renovation process of the carbon dioxide absorbent solution in process for carbon dioxide recovery | |
| CN107741103B (en) | Ammonia water absorption type refrigeration combined carbon trapping device | |
| CN113230832B (en) | CO2 capturing system and method for low-volatile organic pollutant emission | |
| CN104208985B (en) | Fume desulphurization method and system | |
| CN107754568B (en) | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process | |
| CN212166984U (en) | CO2Trapping system | |
| CN105233689B (en) | Organic amine wet flue gas desulphurization and desorption system with high-efficiency and low-energy consumption | |
| CN114713003A (en) | Method for utilizing heat in power plant flue gas CO2 capturing process based on chemical absorption method | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN113101786B (en) | Flue gas carbon dioxide capture system and method based on organic solvent absorption-extraction regeneration cycle | |
| CN219539893U (en) | Carbon dioxide trapping system and carbon dioxide treatment system | |
| CN111054187A (en) | Recovery system and gas recovery method | |
| CN204093274U (en) | Flue gas desulphurization system | |
| CN217410284U (en) | Novel chemical absorption method flue gas CO2 entrapment system | |
| CN218544490U (en) | Flue gas waste heat recovery device of coupling carbon entrapment | |
| KR20140038263A (en) | Apparatus for capturing co2 using chemical solvent | |
| CN114367187A (en) | Carbon dioxide capture system | |
| CN205392117U (en) | Absorption heat pump desulfurization process system of can regenerating | |
| CN114788992A (en) | Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system | |
| CN219518342U (en) | Carbon trapping system for low-concentration carbon dioxide flue gas | |
| CN217526998U (en) | Carbon dioxide capture system | |
| CN116492816B (en) | High CO 2 Loaded absorbent carbon capture desorption system and method | |
| CN116531918B (en) | Energy-saving low-partial pressure carbon dioxide capturing system and method | |
| CN218501310U (en) | Rich solution desorption device of renewable desulfurization process | |
| CN217511525U (en) | Mixed salt decarbonization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |