CN217233613U - Double-pressure carbon recycling and circulating system - Google Patents
Double-pressure carbon recycling and circulating system Download PDFInfo
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- CN217233613U CN217233613U CN202220604858.9U CN202220604858U CN217233613U CN 217233613 U CN217233613 U CN 217233613U CN 202220604858 U CN202220604858 U CN 202220604858U CN 217233613 U CN217233613 U CN 217233613U
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Abstract
The utility model provides a two pressure carbon recovery circulation system, send out including organic rankine cycleElectrical System, CO 2 Recovery system, CO 2 A capture system and a low-pressure water vapor heat exchange system; wherein the utility model discloses utilize two organic working mediums of pressing organic rankine power cycle system mesocycle to retrieve steam-water mixture and CO among the low pressure steam heat transfer system 2 CO in the recovery system 2 The energy of the gas is converted into energy by the added first regenerator and the second regenerator, so that the energy conversion efficiency is improved.
Description
Technical Field
The utility model relates to a belong to the energy-conserving technical field of carbon entrapment, in particular to two pressure carbon recovery circulation systems.
Background
The consumption of fossil energy can generate a large amount of carbon dioxide, and along with the increasing consumption of fossil energy, more and more carbon dioxide is discharged into the atmosphere, so that the concentration of carbon dioxide in the atmosphere is continuously increased.
The emission reduction of carbon dioxide mainly comprises the technologies of improving energy efficiency, using new energy, capturing carbon dioxide and the like. Wherein, the carbon dioxide capture technology after combustion is the most effective carbon dioxide emission reduction method aiming at the current global carbon dioxide maximum emission source, namely the flue gas of a coal-fired power plant. In the conventional technology for capturing carbon dioxide after flue gas combustion, the most widely applied technology is an alcohol amine absorption-heat regeneration process represented by Monoethanolamine (MEA). But do notThe heat required by the analysis of the trapped alcohol amine solution in the carbon trapping process of the power plant needs to be provided by low-pressure steam of about 3bar, the low-pressure steam flows out of the reboiler to form a steam-water mixture, the low-grade heat is often not effectively utilized, and the energy loss is a main reason for causing the large energy consumption of the carbon trapping by the chemical absorption method. At the same time, the CO generated after the analysis of the alcohol amine solution is collected 2 The storage and transportation can be carried out only after the liquid is obtained by pressurization and dehydration, 2-3 compressors are generally adopted for compression, the temperature of each 16 outlets can reach more than 200 ℃, and the compression heat can not be reasonably applied frequently.
Therefore, how to provide a dual-pressure carbon recycling cycle system, which efficiently utilizes the heat in the carbon dioxide recycling and capturing process and reduces the energy consumption is a technical problem that needs to be solved by those skilled in the art.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving one of the technical problem in the correlation technique to a certain extent at least and propose a two pressure carbon recovery circulation system, according to the two organic rankine power cycle make full use of CO of the parallel of the heat source design of different grades 2 The available heat in the process of capture and compression increases the power output of the power plant.
The utility model provides a pair of two carbon recycling circulation system includes at least:
an organic rankine cycle power generation system; the organic working media circulating in the organic Rankine cycle power generation system respectively absorb CO 2 Recovering CO in a system 2 And the heat of the steam-water mixture in the low-pressure steam heat exchange system expands to do work; the organic Rankine cycle power generation system comprises a primary pressure power circulation system and a secondary pressure power circulation system; the primary pressure power circulation system and the secondary pressure power circulation system are provided with a heat exchanger, a turbine, a heat regenerator and a condenser on circulation loops;
the CO is 2 A recovery system; it comprises a pressurizing and heating element for collecting CO 2 After pressurization and heat increment, the heat is exchanged with the organic working medium circulating in the primary pressure power circulation system and then is recycled and stored; and
the CO is 2 A capture system; the CO is 2 Collecting CO in raw material gas by using circulating alcohol amine collecting solution in collecting system 2 And further resolve gas CO 2 Gas CO 2 Through the CO 2 The recovery system recovers and stores.
In some embodiments, a low pressure steam heat exchange system is also included; the low-pressure steam heat exchange system utilizes low-pressure steam to respectively communicate with the organic working medium and the CO circulating in the secondary-pressure power circulation system 2 And (4) carrying out heat exchange on the capture alcohol amine solution in the capture system.
In some embodiments, the primary pressure power cycle system comprises a circulation loop formed by connecting a cold side of a fifth heat exchanger, a first turbine, a hot side of a first heat regenerator, a second condenser and a cold side of the first heat regenerator in sequence; and the steam-water mixture in the low-pressure steam heat exchange system is introduced into a hot side of a fifth heat exchanger to exchange heat with the organic working medium circulating in the primary pressure power circulation system.
In some embodiments, the two-stage pressure power cycle system comprises a cold side of a second heat exchanger, a cold side of a fourth heat exchanger, a second turbine, a second condenser and a cold side of a second regenerator which are connected in sequence to form a cycle loop; wherein said CO 2 Recovery of CO from the system 2 And the heat side of the second heat exchanger and the heat side of the fourth heat exchanger are sequentially introduced to exchange heat with the organic working medium circulating in the secondary pressure power circulation system.
In some embodiments, the CO is 2 The recovery system comprises a passage consisting of an air outlet end of the regeneration tower, a hot side of the second heat regenerator, the flash tank, a hot side of the first heat exchanger, a hot side of the second heat exchanger, a hot side of the third heat exchanger, a hot side of the fourth heat exchanger and the storage device which are connected in sequence.
In some embodiments, the CO is 2 The recovery system also comprises a plurality of gas-liquid separators; gaseous CO 2 After exchanging heat with the organic working medium circulating in the secondary pressure power circulation system, gas CO is carried out by utilizing the gas-liquid separator 2 And (5) separating.
In some embodiments, the CO is 2 The trapping system comprises a primary energy trapping loop and a secondary energy trapping loop; the first-stage energy capturing loop comprises an absorption tower, a cold side of the lean-rich liquid heat exchanger, a regeneration tower, a first outlet of the regeneration tower, a cold side of a reboiler and a hot side of the lean-rich liquid heat exchanger which are sequentially connected to form a circulating loop; the secondary energy capturing loop comprises a second outlet of the regeneration tower, a cold side of the first heat exchanger, a cold side of the third heat exchanger and a circulation loop formed by the regeneration tower which are connected in sequence.
In some embodiments, the CO is 2 The recovery system also comprises a passage formed by connecting the gas outlet of the reboiler and the gas inlet of the regeneration tower.
In some embodiments, the low pressure steam heat exchange system comprises a hot side of the reboiler, a first outlet end of the steam-water mixture, a hot side of the fifth heat exchanger, and a path back to the boiler.
In some embodiments, the low pressure steam heat exchange system further comprises a second outlet end of the steam-water mixture connected to the hot side of the reboiler; and the second outlet end of the steam-water mixture, the pressure reducing valve, the hot side of the sixth heat exchanger and the return boiler form a passage.
Through the technical scheme, the embodiment of the utility model provides a two carbon recycling circulation system that press has following technological effect:
(1) the embodiment of the utility model makes full use of the low-grade heat of the steam-water mixture flowing out of the reboiler, wherein one part is used for preheating rich liquid, and the other part enters the organic Rankine power cycle to generate electric energy;
(2) the embodiment of the utility model takes out a part of semi-barren liquor for recovering CO 2 The compression heat generated in the compression process is beneficial to reducing the trapping energy consumption;
(3) the embodiment of the utility model provides a according to the two organic rankine power cycle make full use of CO of pressing of the parallel of different grade heat source design 2 The available heat in the process of capture and compression increases the power output of the power plant.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic structural diagram of a dual pressure circulation system according to an embodiment of the present invention.
Fig. 2 is a schematic structural diagram of a dual pressure circulation system with the heat exchanger added in fig. 1.
Fig. 3 is a schematic structural diagram of a dual pressure circulation system including a compressor according to an embodiment of the present invention.
Fig. 4 is a schematic structural diagram of a dual pressure circulation system including a gas-liquid separator according to an embodiment of the present invention.
The system comprises an absorption tower 1, a flash tank 2, a regeneration tower 3, a reboiler 4, a pressure reducing valve 5, a lean-rich liquid heat exchanger 6, a rich liquid pump 7, a lean liquid pump 8, a first heat exchanger 9, a second heat exchanger 10, a third heat exchanger 11, a fourth heat exchanger 12, a fifth heat exchanger 13, a sixth heat exchanger 14, a compressor 15, a first turbine 16, a second turbine 17, a gas-liquid separator 18, a semi-lean liquid pump 19, a first heat regenerator 20, a second heat regenerator 21, a first condenser 22, a second condenser 23 and a third condenser 24.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention more clearly understood, the present invention will be described in further detail with reference to the accompanying drawings and detailed description. It should be noted that, in case of conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced in other ways than those specifically described herein, and therefore the scope of the present invention is not limited by the specific embodiments disclosed below.
Example 1
As shown in fig. 1-4, embodiments of the present invention provide a dual pressure carbon recovery cycle system; in which organic Rankine cycle power generation system is circulatedMachine working medium respectively absorbing CO 2 Recovering CO in a system 2 And expanding and applying work after the heat of the steam-water mixture in the low-pressure steam heat exchange system; the organic Rankine cycle power generation system comprises a primary pressure power circulation system and a secondary pressure power circulation system; the first-stage pressure power circulation system and the second-stage pressure power circulation system are respectively provided with a heat exchanger, a turbine, a heat regenerator and a condenser on circulation loops;
CO 2 a recovery system; it comprises a pressurizing and heating part for collecting CO 2 After pressurization and heat increment, the organic working medium is subjected to heat exchange with the organic working medium circulating in the primary pressure power circulation system and then is recycled and stored;
CO 2 a capture system; CO 2 2 Collecting CO in raw material gas by using circulating alcohol amine collecting solution in collecting system 2 And further resolve gas CO 2 Gas CO 2 By CO 2 The recovery system recovers and stores; and
a low pressure steam heat exchange system; organic working medium and CO respectively circulating in secondary pressure power circulation system by using low-pressure water vapor 2 And (4) carrying out heat exchange on the trapping alcohol amine solution in the trapping system.
It is easy to understand that, in the embodiment, an element having a hot side and a cold side such as a heat exchanger or a first heat regenerator is involved, where the hot side and the cold side are both independent cooling pipes and include an input end and an output end, for example, a hot medium to be cooled is introduced from the input end of the hot side, a cold medium to be heated is introduced from the input end of the cold side, after heat exchange is performed between the hot medium and the cold medium, the hot medium after heat exchange is output from the output end of the hot side, and the cold medium after heat exchange is output from the output end of the cold side.
According to an embodiment of the present invention, the first pressure power cycle system comprises a circulation loop formed by the cold side of the fifth heat exchanger 13, the first turbine 16, the hot side of the first heat regenerator 20, the second condenser 23, and the cold side of the first heat regenerator 20, which are connected in sequence; wherein the steam-water mixture in the low-pressure steam heat exchange system is introduced into the hot side of the fifth heat exchanger 13 to exchange heat with the organic working medium circulating in the primary pressure power cycle system.
Specifically, in the embodiment, a cycle working medium of the primary pressure power cycle system in the organic rankine cycle power generation system is an organic working medium, that is, an ORC working medium, wherein the organic working medium passes through the cold side of the fifth heat exchanger 13, and after absorbing heat of a steam-water mixture in the low-pressure steam heat exchange system at the hot side of the fifth heat exchanger 13, the ORC working medium enters the first turbine 16, that is, the ORC turbine, at the time, the pressure of the ORC working medium is 2-3 MPa to perform expansion work. The organic working medium flows out after being evaporated into organic steam in the first turbine 16, is introduced into the hot side of the first heat regenerator 20, exchanges heat with the organic working medium introduced into the cold side of the first heat regenerator 20, is cooled by the second condenser 23, is introduced into the cold side of the first heat regenerator 20, and enters the cold side of the fifth heat exchanger 13 after being preheated, thereby forming a circulation loop.
According to an embodiment of the present invention, the two-stage pressure power cycle system comprises a loop formed by the cold side of the second heat exchanger 10, the cold side of the fourth heat exchanger 12, the cold side of the second turbine 17, the second condenser 23, and the cold side of the second regenerator 21, which are connected in sequence; wherein CO is 2 CO in the recovery system 2 And the hot side of the second heat exchanger 10 and the hot side of the fourth heat exchanger 12 are sequentially introduced to exchange heat with the organic working medium circulating in the secondary pressure power circulation system.
Specifically, in this embodiment, the cycle working medium of the secondary pressure power cycle system in the organic rankine cycle power generation system is an organic working medium, that is, an ORC working medium, wherein the organic working medium passes through the cold side of the second heat exchanger 10 to absorb CO entering the hot side of the second heat exchanger 10 2 CO in the recovery system 2 Enters the cold side of the fourth heat exchanger 12 and absorbs CO entering the hot side of the fourth heat exchanger 12 2 CO in the recovery system 2 After the heat is generated, the pressure of the ORC working medium reaches 1-2MPa, the ORC working medium enters the second turbine 17 (namely the ORC turbine) to perform expansion work, the organic working medium is evaporated into organic steam in the second turbine 17 and then flows out, and the organic working medium is introduced into the second condenser 23 to be cooled into a liquid state so as to be convenient for using a pump to lift the pressure and perform reciprocating circulation. The cooled organic working medium is introduced into the cold side of the second heat regenerator 21 and is cooled by CO at the hot side of the first heat regenerator 20 2 Recovery of CO in a system 2 After heat exchange and preheating, the cold side of the second heat exchanger 10 is entered to form a circulation loop.
According to an embodiment of the present invention, CO 2 The recovery system comprises a passage consisting of an air outlet end of the regeneration tower 3, a hot side of the second heat exchanger 10, the flash tank 2, the hot side of the second heat exchanger 10, the hot side of the fourth heat exchanger 12 and a storage device which are connected in sequence.
Specifically, as shown in FIG. 2, CO 2 The recovery system also comprises a hot side of the first heat exchanger and a hot side of the third heat exchanger, i.e. CO 2 The recovery system comprises a regeneration tower 3 air outlet end, a hot side of a second heat exchanger 10, a flash tank 2, a hot side 9 of a first heat exchanger, a hot side of the second heat exchanger 10, a hot side 11 of a third heat exchanger, a hot side of a fourth heat exchanger 12 and a passage consisting of a storage device, which are sequentially connected.
Specifically, as shown in FIG. 3, CO 2 The recovery system further comprises a plurality of gas-liquid separators 18; gaseous CO 2 After heat exchange with the organic working medium circulating in the secondary pressure power circulating system.
CO in this example 2 The number of the pressurizing and heating members in the recovery system is several, and the pressurizing and heating members can be understood as a compressor 15 for CO 2 Before heat exchange of circulating semi-barren solution in the capture system, the gas compressor 15 is required to be used for gas CO 2 Pressurizing and heating.
Understandably, the gaseous CO in the regeneration column 3 2 Enters the hot side of the second heat regenerator 21 through the gas outlet end of the regeneration tower 3, exchanges heat with the organic working medium of the cold-side secondary pressure power cycle system passing through the second heat regenerator 21, enters the flash tank 2 and recovers the CO gas again 2 Gas CO 2 After being pressurized by the compressor 15, the CO flows into the hot side of the first heat exchanger 9 and the CO at the cold side of the first heat exchanger 9 2 After the heat exchange of the circulating semi-lean solution in the capture system, the semi-lean solution is introduced into the hot side of the second heat exchanger 10, and after the heat exchange with the organic working medium of the secondary pressure power cycle system at the cold side of the second heat exchanger 10, the semi-lean solution is subjected to gas-liquid separation by the gas-liquid separator 18, a small amount of separated water can be directly discharged, and gas CO can be directly discharged 2 The CO is pressurized again by the compressor 15 and then is introduced into the hot side of the third heat exchanger 11 and the CO at the cold side of the third heat exchanger 11 2 After the heat exchange of the circulating semi-lean solution in the capture system, the semi-lean solution is introduced into the hot side of the fourth heat exchanger 12 to be communicated with the fourth heat exchanger12, the gas-liquid separator 18 is used for gas-liquid separation again after the heat exchange of the organic working medium circulated by the secondary pressure power cycle system at the cold side of the heat exchanger 12, a small amount of separated water can be directly discharged, and the separated gas CO can be directly discharged 2 Finally, the gas is introduced into a third condenser 24 for condensation, and then the nitrogen gas of the gas in the separation tank is discharged and stored, and the condensed liquid CO 2 In the storage device, as shown in fig. 4.
According to an embodiment of the present invention, CO 2 The trapping system comprises a primary energy trapping loop and a secondary energy trapping loop; the primary energy capturing loop comprises a circulating loop consisting of an absorption tower 1, a cold side of a lean-rich liquid heat exchanger 6, a regeneration tower 3, a first outlet of the regeneration tower 3, a cold side 4 of a reboiler and a hot side of the lean-rich liquid heat exchanger 6 which are connected in sequence; the secondary energy capture loop comprises a circulation loop consisting of the second outlet of the regeneration tower 3, the cold side of the first heat exchanger 9, the cold side of the third heat exchanger 11 and the regeneration tower which are connected in sequence.
A first condenser 22 is further included in the preferred primary energy capture circuit, as shown in fig. 2, wherein the first condenser 22 is disposed between the lean-rich liquid heat exchanger 6 and the absorber column 1 for cooling the refluxed lean liquid.
In this embodiment, the raw material gas is flue gas of a power plant, a chemical plant or an iron and steel plant, and specifically, the content of carbon dioxide is 5% to 25%. The preferred carbon dioxide content is 10%, and the alcohol amine trapping solution in this example is an MEA/MDEA solution.
In the embodiment of the present invention, the dual-pressure organic rankine power cycle system for recovering carbon capture energy includes: CO in this example 2 The alcohol amine solution for trapping in the trapping system is MEA/MDEA solution which is in CO 2 The internal fluid flow conditions in the trapping system were: the MEA/MDEA solution enters the absorption tower 1 through the liquid inlet end of the absorption tower 1, meanwhile, the raw material gas enters through the gas inlet end of the absorption tower 1, and the MEA/MDEA solution absorbs CO gas in the raw material gas 2 The clean flue gas is discharged through the gas outlet end of the absorption tower 1, and the gas CO is discharged 2 Dissolving in MEA/MDEA solution which is MEA/MDEA rich solution, and passing through absorption tower 1Discharging from the liquid outlet end. The MEA/MDEA rich solution is pressurized by a rich solution pump 7, then exchanges heat with the steam-water mixture in the low-pressure steam heat exchange system through the cold side of a sixth heat exchanger 14, is preheated, then enters the cold side of a lean rich solution heat exchanger 6 for heating, finally enters a regeneration tower 3 through an MEA/MDEA rich solution inlet of the regeneration tower 3, and generates CO gas after heating and analysis 2 The MEA/MDEA rich solution is changed into an MEA/MDEA semi-lean solution, a part of the MEA/MDEA semi-lean solution enters the cold side of a reboiler 4 through a first outlet of a regeneration tower 3, and after heat exchange is carried out through low-pressure steam at the hot side of the reboiler 4, CO gas in the MEA/MDEA semi-lean solution 2 And after all the solutions are converted into MEA/MDEA lean solution, the MEA/MDEA lean solution enters the hot side of the lean and rich solution heat exchanger 6, the MEA/MDEA rich solution entering from the cold side of the lean and rich solution heat exchanger 6 is preheated, pressurized by a lean solution pump 8, introduced into the hot side of the first condenser 22, cooled by cooling water and introduced into the absorption tower 1.
To further optimize the present embodiment, the secondary energy capture circuit is specifically understood as: another part of the MEA/MDEA semi-barren solution enters the cold side of the first heat exchanger 9 through a second outlet of the regeneration tower 3 and enters the gas CO at the hot side of the first heat exchanger 9 2 After heat exchange, absorbing heat, and introducing the cold side of the third heat exchanger 11; again with the hot side CO entering the third heat exchanger 11 2 The CO gas after pressurization and heat increment in the recovery system 2 Heat exchange, after the pressure is increased by a semi-barren liquor pump 19, the semi-barren liquor enters a regeneration tower 3 through a semi-barren liquor inlet of the regeneration tower 3 to form a circulation loop.
In the embodiment, a half lean solution is extracted from the middle part of the regeneration tower to absorb two compression heat generated by 16, and then the half lean solution is sent back to the regeneration tower 3 by the half lean solution pump 19, so that the extraction amount is reduced, the carbon capture energy consumption is reduced, and the residual compression heat is absorbed by the organic working medium.
According to an embodiment of the present invention, CO 2 The recovery system also comprises a path consisting of the gas outlet of the reboiler 4 and the gas inlet of the regeneration column 3.
From the above examples, it can be seen that the gaseous CO in the MEA/MDEA semi-lean solution entering the reboiler 4 2 Passes through an air outlet of a reboiler 4,The gas inlet of the regeneration tower 3 enters the regeneration tower 3.
According to the utility model discloses an embodiment, low pressure steam heat transfer system includes the hot side of reboiler 4, the first exit end of steam-water mixture, the hot side of fifth heat exchanger 13 and the route of returning the boiler to constitute.
According to the utility model discloses an embodiment, low pressure steam heat transfer system still includes the steam-water mixture second exit end of being connected with the hot side of reboiler 4, wherein another route that hot side, steam-water mixture second exit end, relief pressure valve 5, the hot side of sixth heat exchanger 14 and the boiler of returning of reboiler 4 constitute
According to the embodiment of the utility model, be used for retrieving two pressure organic rankine power cycle systems of carbon entrapment energy, include steam-water mixture first exit end and steam-water mixture second exit end among the low pressure steam heat transfer system on reboiler 4, divide into two branches with steam-water mixture, wherein steam-water mixture gets into the hot side of fifth heat exchanger 13 through steam-water mixture first exit end, after the heat transfer with the first-order pressure power cycle system endless organic working medium that gets into the cold side of fifth heat exchanger 13, lets in back the boiler; and the steam-water mixture enters the pressure reducing valve 5 through a second outlet end of the steam-water mixture, after the steam-water mixture is subjected to pressure reduction, the steam-water mixture is introduced into the hot side of the sixth heat exchanger 14 to heat the MEA/MDEA rich solution passing through the cold side of the sixth heat exchanger 14, and then the steam-water mixture is cooled and introduced back to the boiler.
The heat required by rich liquid analysis in the carbon capture process of the power plant needs to be provided by low-pressure water vapor of about 3bar, the low-pressure water vapor flows out of the reboiler 4 to form a steam-water mixture, the low-grade heat is often not effectively utilized, a part of the steam-water mixture enters the pressure reducing valve 5 through the second outlet end of the steam-water mixture to be reduced in pressure to improve the gas phase fraction, the steam-water mixture after being reduced in pressure is used for preheating MEA/MDEA rich liquid after being pressurized by the rich liquid pump 7, therefore, the phase change heat of the steam in the steam-water mixture can be utilized to a greater extent, the temperature of the rich liquid entering the regeneration tower 3 is improved, more low-grade heat is used in the carbon capture process through the method, the steam extraction amount of the low-pressure steam can be reduced, the loss of the higher-grade heat is reduced, and finally, the loss of the higher-grade heat is reducedReducing energy consumption of the power plant in the carbon capture process. The heat carried by the other part of the steam-water mixture which flows out through the second outlet end of the steam-water mixture and is not decompressed is also larger, so that the organic working medium is provided with higher boosting pressure and a first heat regenerator to improve the energy conversion efficiency. Due to the decomposition of CO gas 2 The flow rate of the gas-water mixture is less than that of the steam-water mixture, so that the pressure of the organic working medium of the secondary pressure power cycle system is lower, the sensible heat of the analyzed gas and the residual compression heat of the compressor are absorbed after the organic working medium is pressurized by the pump, and then the organic working medium enters the second turbine 17 to do work. And cooling the organic working medium after the work is done, and then performing power circulation again.
The method for recovering the carbon capture energy by using the device comprises the following steps:
the MEA/MDEA solution enters the absorption tower 1 through the liquid inlet end of the absorption tower 1, meanwhile, the raw material gas enters through the gas inlet end of the absorption tower 1, and the MEA/MDEA solution absorbs CO gas in the raw material gas 2 The clean flue gas is discharged from the gas outlet end of the absorption tower 1, and the gas CO is discharged 2 The solution is dissolved in MEA/MDEA solution, the MEA/MDEA solution is discharged from the liquid outlet end of the absorption tower 1, enters the cold side of a sixth heat exchanger 14 through a rich liquid pump 7 to exchange heat with the steam-water mixture in a low-pressure steam heat exchange system, preheats the MEA/MDEA rich solution, then enters the cold side of a lean rich solution heat exchanger 6 to be heated, finally enters a regeneration tower 3 through a rich solution inlet of the regeneration tower 3, and generates CO gas after heating and analysis 2 Enters the hot side of the second heat regenerator 21 through the air outlet end of the regeneration tower 3, exchanges heat with the organic working medium of the cold-side secondary pressure power cycle system passing through the second heat regenerator 21, enters the flash tank 2 and recovers the CO gas again 2 Gas CO 2 After being pressurized by the compressor 15, the CO flows into the hot side of the first heat exchanger 9 and the CO at the cold side of the first heat exchanger 9 2 After heat exchange is carried out on the circulating semi-lean solution in the capture system, the semi-lean solution is introduced into the hot side of the second heat exchanger 10, exchanges heat with the organic working medium of the secondary pressure power cycle system at the cold side of the second heat exchanger 10, and then gas-liquid separation is carried out on the semi-lean solution in the gas-liquid separator 18, a small amount of separated water can be directly discharged, and CO gas is directly discharged 2 Pressurized again by the compressor 15 and then introduced into the hot side of the third heat exchanger 11 and the hot side of the third heat exchanger 11CO at the cold side 2 After the heat exchange of the circulating semi-lean solution in the capturing system, the semi-lean solution is introduced into the hot side of the fourth heat exchanger 12, the semi-lean solution exchanges heat with the circulating organic working medium of the secondary pressure power circulation system at the cold side of the fourth heat exchanger 12, the gas-liquid separator 18 is used for gas-liquid separation again, a small amount of separated water can be directly discharged, and the separated gas CO can be directly discharged 2 Finally, the third condenser 24 is connected for condensation, the gas is introduced into a separation tank, the nitrogen of the gas is discharged and stored, and the condensed liquid CO 2 In the storage device.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", and the like, indicate the orientation or positional relationship indicated based on the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and "fixed" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
In the present application, unless expressly stated or limited otherwise, the first feature may be directly on or directly under the second feature or indirectly via intermediate members. Also, a first feature "on," "above," and "over" a second feature may be directly on or obliquely above the second feature, or simply mean that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" or the like mean 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 present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (10)
1. A dual pressure carbon recovery cycle system, comprising:
an organic rankine cycle power generation system; the organic working media circulating in the organic Rankine cycle power generation system respectively absorb CO 2 Recovering CO in a system 2 And the heat of the steam-water mixture in the low-pressure steam heat exchange system expands to do work; the organic Rankine cycle power generation system comprises a primary pressure power circulation system and a secondary pressure power circulation system; the primary pressure power circulation system and the secondary pressure power circulation system are provided with a heat exchanger, a turbine, a heat regenerator and a condenser on circulation loops;
the CO is 2 A recovery system; it comprises a pressurizing and heating part for collecting CO 2 After pressurization and heat increment, the heat is exchanged with the organic working medium circulating in the primary pressure power circulation system and then is recycled and stored; and
the CO is 2 A capture system; the CO is 2 Collecting CO in raw material gas by using circulating alcohol amine collecting solution in collecting system 2 And further resolve gas CO 2 Gas CO 2 Through the CO 2 The recovery system recovers and stores.
2. The circulation system of claim 1, further comprising a low pressure steam heat exchange system; the low-pressure steam heat exchange system utilizes low-pressure steam to respectively communicate with the organic working medium and the CO circulating in the secondary-pressure power circulation system 2 And (4) carrying out heat exchange on the capture alcohol amine solution in the capture system.
3. The circulation system of claim 2, wherein the primary pressure power circulation system comprises a circulation loop formed by connecting a cold side of a fifth heat exchanger, the first turbine, a hot side of a first heat regenerator, the second condenser and a cold side of the first heat regenerator in sequence; and the steam-water mixture in the low-pressure steam heat exchange system is introduced into the hot side of a fifth heat exchanger to exchange heat with the organic working medium circulating in the primary pressure power circulation system.
4. The circulation system as set forth in claim 2,the system is characterized in that the two-stage pressure power cycle system comprises a cold side of a second heat exchanger, a cold side of a fourth heat exchanger, and a cycle loop formed by a second turbine, a second condenser and a cold side of a second heat regenerator which are sequentially connected; wherein said CO 2 CO in the recovery system 2 And the heat side of the second heat exchanger and the heat side of the fourth heat exchanger are sequentially introduced to exchange heat with the organic working medium circulating in the secondary pressure power circulation system.
5. The circulation system of claim 2, wherein the CO is present in the gas supply system 2 The recovery system comprises a path consisting of an air outlet end of the regeneration tower, a hot side of the second heat regenerator, the flash tank, the hot side of the second heat exchanger, the hot side of the fourth heat exchanger and the storage device which are connected in sequence.
6. The circulation system of claim 5, wherein the CO is in the form of a CO 2 The recovery system also comprises a plurality of gas-liquid separators; gaseous CO 2 After exchanging heat with the organic working medium circulating in the secondary pressure power circulation system, gas CO is carried out by utilizing the gas-liquid separator 2 And (5) separating.
7. The circulation system of claim 3, wherein the CO is present in the gas supply system 2 The trapping system comprises a primary energy trapping loop and a secondary energy trapping loop; the first-stage energy capturing loop comprises an absorption tower, a cold side of the lean-rich liquid heat exchanger, a regeneration tower, a first outlet of the regeneration tower, a cold side of a reboiler and a hot side of the lean-rich liquid heat exchanger which are sequentially connected to form a circulating loop; the secondary energy capturing loop comprises a second outlet of the regeneration tower, the cold side of the first heat exchanger, the cold side of the third heat exchanger and a circulation loop formed by the regeneration tower, which are connected in sequence.
8. The circulation system of claim 7, wherein the CO is present in the gas supply system 2 The recovery system also comprises a passage formed by connecting the gas outlet of the reboiler and the gas inlet of the regeneration tower.
9. The circulation system of claim 3, wherein the low pressure steam heat exchange system comprises a path consisting of the hot side of the reboiler, the first outlet end of the steam-water mixture, the hot side of the fifth heat exchanger, and the boiler return.
10. The circulation system of claim 8, wherein the low pressure steam heat exchange system further comprises a second outlet port for steam-water mixture connected to the hot side of the reboiler; and the second outlet end of the steam-water mixture, the pressure reducing valve, the hot side of the sixth heat exchanger and the boiler form a passage.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220604858.9U CN217233613U (en) | 2022-03-17 | 2022-03-17 | Double-pressure carbon recycling and circulating system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220604858.9U CN217233613U (en) | 2022-03-17 | 2022-03-17 | Double-pressure carbon recycling and circulating system |
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