CN114712990B - CO (carbon monoxide) 2 Regeneration device and process method - Google Patents
CO (carbon monoxide) 2 Regeneration device and process method Download PDFInfo
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- CN114712990B CN114712990B CN202210268006.1A CN202210268006A CN114712990B CN 114712990 B CN114712990 B CN 114712990B CN 202210268006 A CN202210268006 A CN 202210268006A CN 114712990 B CN114712990 B CN 114712990B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The embodiment of the invention provides a CO 2 Regeneration device and process method, CO 2 The regeneration device comprises: CO 2 Recovery system, CO 2 A double-tower trapping system and a low-pressure water vapor heat exchange system; embodiments of the invention utilize captured alcohol amine solution MEA/MDEA in CO 2 Adsorption of CO in feed gas in a double tower trap system 2 The CO is respectively analyzed and recovered by the first trapping system and the second trapping system, and the analyzed CO is analyzed 2 Through CO 2 The recovery system stores.
Description
Technical Field
The invention relates to a carbon trapping energy-saving technologyThe field relates to a CO 2 Regeneration device and process method.
Background
The consumption of fossil energy generates 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. The technology for capturing carbon dioxide after combustion is the most effective carbon dioxide emission reduction method for the flue gas of the coal-fired power plant, which is the current global carbon dioxide maximum emission source. In the conventional carbon dioxide capturing technology after flue gas combustion, the most widely used is an alcohol amine absorption-thermal regeneration process represented by Monoethanolamine (MEA). However, the heat required by the analysis of the alcohol amine rich solution in the carbon capture process of the power plant is required to be provided by low-pressure steam of about 3bar, the low-pressure steam flows out of a reboiler to become a steam-water mixture, the low-grade heat is often not effectively utilized, and the energy loss is a main reason for larger energy consumption of carbon capture by a chemical absorption method. Meanwhile, CO generated after alcohol amine rich solution is resolved 2 The storage and transportation can be carried out after the water is removed by pressurization and changed into a liquid state, and the storage and transportation can be carried out by adopting 2-3 compressors, wherein the temperature of the output end of each 16 can reach more than 200 ℃, and the compression heat can not be reasonably utilized.
Thus, how to provide a CO 2 Regeneration device and process method, heat in carbon dioxide recovery and trapping process is efficiently utilized, energy consumption is reduced, and CO is enhanced 2 Regeneration is a technical problem that needs to be solved by those skilled in the art.
Disclosure of Invention
The invention aims to solve one of the technical problems in the related art to at least a certain extent and provides a CO 2 The regeneration device and the process method can flexibly regulate and control the gas phase fraction of the steam-water mixture flowing out of the reboiler by regulating the pressure of the output end of the pressure reducing valve, and the steam is liquefied and complemented with the lost water after entering the flash evaporation tower to preheat the alcohol amine solution, and the liquid water heats part of alcoholThe amine solution was used for preliminary resolution. In addition, the water vapor and the heat carried by the water vapor are recovered from the alcohol amine lean solution flowing out of the reboiler by decompression, the alcohol amine lean solution is sent back to the regeneration tower after being properly pressurized, the water vapor and the heat are recovered, and the temperature of the alcohol amine lean solution after decompression is reduced, so that the heat exchange is fully performed in the subsequent heat exchange process.
The invention provides a CO 2 A regeneration device comprising:
CO 2 double tower capture system, said CO 2 The double-tower trapping system comprises a circulating passage consisting of a first trapping system and a second trapping system, wherein the trapping alcohol amine solution circulating in the first trapping system and the second trapping system firstly absorbs CO in the raw gas 2 And then the trapped CO 2 Analysis, analysis of CO 2 Through the CO 2 The recovery system is used for recovery and storage;
CO 2 recovery system of the CO 2 The recovery system recovers CO 2 Analytic CO that produces of double tower entrapment system 2 Storing after enrichment and recovery; and
the low-pressure water vapor heat exchange system comprises a first water vapor heat exchange system and a second water vapor heat exchange system; the first water vapor heat exchange system and the second water vapor heat exchange system both use low-pressure water vapor as heat mediums, and the low-pressure water vapor respectively heats the trapping alcohol amine solution circulated in the first trapping system and the second trapping system and supplements water in the first trapping system and the second trapping system.
In some embodiments, the first capture system comprises a pathway comprised of the cold side of an absorber, a flash column, and a lean rich liquid heat exchanger connected in sequence.
In some embodiments, the first capture system comprises a passageway comprising the cold side of the second reboiler, the first gas-liquid separator, and the output of the cold side of the lean-rich liquid heat exchanger connected in sequence; the cold side input of the second reboiler is connected to the flash column.
In some embodiments, the second capture system comprises a pass consisting of a regeneration column, a cold side of the first reboiler, a hot side of the lean-rich liquid heat exchanger, and a liquid inlet end of the absorption column connected in sequence; wherein the output end of the cold side of the lean rich liquid heat exchanger is connected with the regeneration tower.
In some embodiments, the CO 2 The recovery system comprises a passage formed by a gas output port of the regeneration tower, a first gas inlet of the flash tower, a gas output port of the flash tower and a storage device which are sequentially connected.
In some embodiments, the CO 2 The recovery system comprises a recovery passage consisting of a gas output port of the first gas-liquid separator and a second gas inlet of the flash tower.
In some embodiments, the CO 2 The recovery system comprises a recovery passage consisting of a gas output port of the first reboiler and a gas input port of the regeneration tower; wherein the cold side of the first reboiler is connected with the liquid outlet of the regeneration tower.
In some embodiments, the first water vapor heat exchange system comprises a passageway comprising a hot side of a first reboiler, a second pressure reducing valve, and a third gas-liquid separator connected in sequence; the second water vapor heat exchange system comprises a passage formed by the hot side of a second reboiler and a boiler; wherein the gas output port of the third gas-liquid separator is connected with the third gas inlet of the flash tower; the hot side input end of the second reboiler is connected with the liquid outlet of the third gas-liquid separator.
In some embodiments, a method of enhancing CO 2 The regeneration process method, by using the device in any embodiment, comprises the following steps:
capturing CO in alcohol amine solution absorbing raw material gas 2 Obtaining alcohol amine rich liquid;
after preliminary analysis of the alcohol amine rich solution in the flash tower, the alcohol amine rich solution with the volume percentage of 9-12% enters a second reboiler for heating and analysis to generate CO 2 And alcohol amine semi-rich liquid, CO 2 Introducing the alcohol amine semi-rich liquid and the rest of the heated alcohol amine rich liquid into a flash tower, mixing and pressurizing, and then, introducing the mixture into a regeneration tower for deep analysis;
the alcohol amine semi-rich liquid enters a first reboiler to be heated and resolved to generate CO 2 And alcohol amine lean solution, CO 2 Introducing the CO into the regeneration tower and resolving the CO with the regeneration tower 2 Introducing the mixture into a flash tower for heat exchange, and performing CO (carbon monoxide) heat exchange 2 Collecting and storing;
and the alcohol amine lean solution is decompressed and then subjected to heat exchange and circulated to the absorption tower.
In some embodiments, the alcohol amine rich liquid is controlled to have a resolution temperature of 90-110 ℃ and a pressure of 0.8-1.5bar in the flash column; the resolving temperature of the second water vapor heat exchange system is 115-130 ℃ and the pressure is 2-3bar; the resolving temperature of the regeneration tower is 115-130 ℃ and the pressure is 2-3bar; the resolving temperature of the first water vapor heat exchange system is 90-110 ℃, and the pressure is 0.8-1.5bar.
Through the technical scheme, the invention provides the CO 2 The regeneration device, the process method and the technological method have the following technical effects:
(1) The water loss in the carbon trapping process is supplemented by the water vapor with higher temperature, which is beneficial to reducing the heat loss;
(2) Multiple strands of gases with higher temperature are introduced into a flash tower to perform direct contact type convection heat exchange with rich liquid, so that cooling loss in the carbon capturing process is effectively reduced;
(3) The lean solution at the output end of the reboiler is compressed and sent back to the regeneration tower after flash evaporation, which is beneficial to reducing heat consumption;
(4) A small amount of carbon dioxide is regenerated by utilizing low-grade heat of the steam-water mixture, so that the steam extraction quantity is reduced finally, and the thermal efficiency of the power plant is improved.
Drawings
The foregoing and/or additional aspects and advantages of the invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings, in which:
FIG. 1 is a schematic diagram of a CO system according to one embodiment of the present invention 2 The structure of the regenerating device is schematically shown.
FIG. 2 is the CO addition in example 1 2 The structure of the regeneration device of the recovery passage is schematically shown.
Fig. 3 is a schematic structural view of a regeneration device including a water vapor recovery system according to an embodiment of the present invention.
FIG. 4 is a diagram of enhanced CO provided by one embodiment of the present invention 2 A regeneration process flow chart.
The device comprises a 1-absorption tower, a 2-flash tower, a 3-regeneration tower, a 4-first reboiler, a 5-second reboiler, a 6-lean-rich liquid heat exchanger, a 7-second pressure reducing valve, an 8-lean liquid pump, a 9-first pressure reducing valve, a 10-first gas-liquid separator, a 11-second gas-liquid separator, a 12-third gas-liquid separator, a 13-first rich liquid pump, a 14-second rich liquid pump, a 15-gas compressor, a 16-storage device, a 17-boiler and a 18-condenser.
Detailed Description
In order that the above-recited objects, features and advantages of the present invention will be more clearly understood, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description. It should be noted that, without conflict, the embodiments of the present invention and features in 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 described herein, and therefore the scope of the present invention is not limited to the specific embodiments disclosed below.
Example 1
In this embodiment, the raw material gas is power plant flue gas, chemical plant flue gas or steel plant flue gas, and specifically, the carbon dioxide content is 5% -25%. In this example, the alcohol amine trapping solution was MEA/MDEA solution to adsorb CO in the feed gas 2 . In the embodiment, the heat exchanger or the first reboiler and other elements with hot side and cold side are provided, wherein the hot side and the cold side are independent cooling pipes and comprise an input end and an output end, for example, a heat medium needing to be cooled is introduced from the input end of the hot side, a cold medium needing to be warmed is introduced from the input end of the cold side, after heat exchange is carried out on the heat medium and the cold medium, the heat 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.
As shown in fig. 1, the present embodiment proposes a CO 2 A regeneration device comprising: CO 2 Recovery system, CO 2 A double-tower trapping system and a low-pressure water vapor heat exchange system; CO using a trapping alcohol amine solution, namely MEA/MDEA solution 2 Adsorption of feed gas in a double tower trap systemCO in (b) 2 The CO is respectively analyzed and recovered by the first trapping system and the second trapping system, and the analyzed CO is analyzed 2 Through CO 2 The recovery system stores.
In some embodiments, the CO 2 The double-tower trapping system comprises a circulating passage consisting of a first trapping system and a second trapping system, and the trapping alcohol amine solution circulating in the first trapping system and the second trapping system absorbs CO in the raw material gas 2 Obtaining an MEA/MDEA rich solution, and analyzing and recovering CO in the MEA/MDEA rich solution through a first trapping system and a second trapping system respectively 2 Resolved CO 2 Through CO 2 The recovery system stores. The first trapping system not only comprises a passage formed by the cold sides of the absorption tower 1, the flash tower 2 and the lean-rich liquid heat exchanger 6 which are connected in sequence, but also comprises a passage formed by the cold side of the second reboiler 5, the liquid outlet of the first gas-liquid separator 10 and the output end of the cold side of the lean-rich liquid heat exchanger 6 which are connected in sequence; the cold side input of the second reboiler 5 is connected to the flash column 2.
Advantageously, a first rich liquor pump 13 is also included between the liquid outlet end of the absorption column 1 and the flash column 2, and the MEA/MDEA solution absorbs CO in the raw material gas in the absorption column 1 2 An MEA/MDEA rich solution is formed, and the MEA/MDEA rich solution is transported in a pressurizing way through a first rich solution pump 13.
Wherein the first trapping system can be specifically understood as: CO in the present embodiment 2 The alcohol amine rich solution in the trapping system is MEA/MDEA solution, and the MEA/MDEA solution is prepared in CO 2 The internal fluid flow conditions in the trapping system are: the MEA/MDEA solution enters through the liquid inlet end of the absorption tower 1, and meanwhile, the raw gas enters through the gas inlet of the absorption tower 1 and absorbs CO in the raw gas through the MEA/MDEA solution 2 The gas, clean flue gas is discharged through the gas outlet of the absorption tower 1, and CO 2 The gas is dissolved in the MEA/MDEA solution, the MEA/MDEA solution is MEA/MDEA rich solution at the moment, the MEA/MDEA rich solution is discharged from the liquid outlet end of the absorption tower 1, the gas is pressurized by the first rich solution pump 13 and enters the flash tower 2 for analysis, and the analysis process can be controlled by adjusting the flash pressure of the flash tower 2 until the CO analyzed in the flash tower 2 2 The regulation of the flash pressure is stopped when the gas is unchanged.Through Aspen Plus simulation, CO is resolved in the flash column 2 2 Occupying all resolved CO 2 By 5% -7% of the steam turbine, the extraction amount of the steam turbine of the power plant can be reduced by reasonably utilizing the low-grade heat of the steam, so that more high-grade steam is prevented from being pumped, and the purpose of reducing the energy loss of the power plant is achieved.
The MEA/MDEA solution rich solution after being resolved by the flash tower 2 enters the cold side of the second reboiler 5 with the volume percentage of 9% -12% (preferably 9%,10%,11%, 12%), the MEA/MDEA rich solution is heated and resolved by low-pressure steam on the hot side of the second reboiler 5 to become MEA/MDEA semi-rich solution, the MEA/MDEA semi-rich solution is introduced into the first gas-liquid separator 10 for gas-liquid separation, and the separated CO is separated 2 The gas is passed to flash column 2 and the mea/MDEA semi-rich liquid is passed to the cold side output of lean rich liquid heat exchanger 6. And the rest MEA/MDEA rich liquid after being analyzed by the flash tower 2 enters the cold side of the lean-rich liquid heat exchanger 6, exchanges heat with the MEA/MDEA lean liquid at the hot side of the lean-rich liquid heat exchanger 6, flows out from the output end of the cold side of the lean-rich liquid heat exchanger 6, is converged with the MEA/MDEA semi-rich liquid, and is introduced into a second trapping system.
The second trapping system comprises a passage formed by a regeneration tower 3, a cold side of a first reboiler 4, a hot side of a lean-rich liquid heat exchanger 6 and a liquid inlet end of an absorption tower 1 which are connected in sequence; wherein the cold side output of the lean-rich liquid heat exchanger 6 is connected to the regenerator 3.
Advantageously, the second capturing system further comprises a second rich liquid pump 14, after the MEA/MDEA rich liquid at the cold side output end of the lean-rich liquid heat exchanger 6 is converged with the MEA/MDEA semi-rich liquid, the MEA/MDEA rich liquid is transported into the regeneration tower 3 for further analysis by pressurization of the second rich liquid pump 14, the analyzed MEA/MDEA rich liquid is changed into MEA/MDEA semi-rich liquid, flows out of the regeneration tower 3 and enters the cold side of the first reboiler 4, and after heat exchange is carried out with low-pressure water vapor entering the hot side of the first reboiler 4, CO in the MEA/MDEA semi-rich liquid 2 The gas escapes into the regeneration tower 3 for enrichment, and the MEA/MDEA semi-rich liquid is changed into MEA/MDEA lean liquid which enters the hot side of the lean-rich liquid heat exchanger 6.
Advantageously, the second capturing system further comprises a lean liquid pump 8, and after the MEA/MDEA lean liquid enters the hot side of the lean-rich liquid heat exchanger 6 and exchanges heat with the MEA/MDEA rich liquid on the cold side of the lean-rich liquid heat exchanger 6, the MEA/MDEA lean liquid is conveyed by the lean liquid pump 8 and mixed with the external supplementary MEA/MDEA solution, and then the mixture is introduced into the liquid inlet end of the absorption tower 1 and flows back to the absorption tower 1.
Alternatively, a condenser 18 may be provided in the path between the lean solution pump 8 and the absorption column 1, and the MEA/MDEA lean solution is mixed with the externally replenished MEA/MDEA solution, cooled by the condenser 18, and then introduced into the liquid inlet end of the absorption column 1.
In some embodiments, the second capturing system further comprises a first pressure reducing valve 9 and a second gas-liquid separator 11, wherein the first pressure reducing valve 9 is arranged between the first reboiler 4 and the second gas-liquid separator 11, and an output end of the second gas-liquid separator 11 is connected to an input end of the hot side of the lean-rich liquid heat exchanger 6.
Specifically, as shown in fig. 3, it can be seen from the above that the MEA/MDEA semi-rich liquid enters the cold side of the first reboiler 4, and after being heated with low pressure steam on the hot side of the first reboiler 4, the CO in the MEA/MDEA semi-rich liquid 2 Gas escapes; the MEA/MDEA lean solution can be depressurized through the first depressurization valve 9, the gas phase fraction of the vapor-water mixture in the MEA/MDEA lean solution is increased, the temperature is reduced, and the vapor can be further compressed to 2-3bar through the second gas-liquid separator 11 so as to match the regeneration pressure of the regeneration tower 3, and the temperature is close to 200 ℃ and then sent back to the regeneration tower 3. The heat of water vapor in the MEA/MDEA lean liquid is recovered on one hand, and the temperature of the MEA/MDEA lean liquid is reduced through depressurization, so that the MEA/MDEA lean liquid can fully absorb the heat in the subsequent heat exchange process.
In some embodiments CO 2 The recovery system comprises a passage formed by a gas output port of the regeneration tower 3, a first gas inlet of the flash tower 2 and a storage device 16 which are connected in sequence; the recovery passage is formed by a gas output port of the first gas-liquid separator 10 and a second gas inlet of the flash tower 2; the device also comprises a recovery passage consisting of a gas output port of the first reboiler 4 and a gas inlet of the regeneration tower 3; wherein the cold side input end of the first reboiler 4 is connected with the liquid outlet of the regeneration tower 3.
As shown in particular in fig. 2, the MEA/MDEA semi-rich liquid enters the cold side of the first reboiler 4,after heating with low pressure steam on the hot side of the first reboiler 4, CO in the MEA/MDEA semi-rich liquid 2 The gas escapes, enters the regeneration tower 3 from the gas inlet of the regeneration tower 3 through the gas outlet of the first reboiler 4, and directly analyzes the CO obtained by MEA/MDEA rich liquid in the regeneration tower 3 2 After mixing the gases (90 ℃), the gases are introduced into the first inlet of the flash column 2 through the gas outlet of the regeneration column 3. Meanwhile, according to the above, 9-12% of MEA/MDEA rich liquid by volume enters the cold side of the second reboiler, and after being heated by low-pressure water vapor on the hot side of the second reboiler, the MEA/MDEA rich liquid is resolved, and is introduced into the first gas-liquid separator 10 through the gas outlet of the second reboiler for gas-liquid separation, wherein the separated CO 2 The gas is introduced into the flash tower 2 through a second gas inlet of the flash tower 2, and CO in the flash tower 2 2 The gas is directly contacted with the MEA/MDEA rich solution for convective heat transfer, and enters the storage device 16 after preheating and preliminary analysis of the MEA/MDEA rich solution. Wherein the storage device 16 is operable for CO 2 The gas is stored after being compressed.
In some embodiments, the first water vapor heat exchange system comprises a passage consisting of a hot side of the first reboiler 4, a second pressure reducing valve 7 and a third gas-liquid separator 12 connected in sequence; the second steam heat exchange system comprises a passage consisting of the hot side of the second reboiler 5 and the boiler 17; wherein the gas output port of the third gas-liquid separator 12 is connected with the third gas inlet of the flash column 2; the hot side of the second reboiler 5 is connected to the liquid outlet of the third gas-liquid separator 12.
Specifically, as shown in fig. 2, low-pressure steam of 3bar enters the hot side of the first reboiler 4 to exchange heat, is depressurized through the second pressure reducing valve 7, increases the specific gravity of the steam in the steam-water mixture, and then enters the third gas-liquid separator 12 to separate the steam from liquid water. The separated vapor is introduced into the third air inlet of the flash tower 2, so that the MEA/MDEA rich liquid with lower temperature in the flash tower 2 can be subjected to heat convection, and can be rapidly liquefied into liquid water after heat exchange, and the water lost in the trapping process can be supplemented. Furthermore, the flow control of the water vapor can be realized by controlling the pressure of the output end of the second pressure reducing valve 7, the water vapor can liquefy and release phase change heat after entering the flash tower 2, and finally the water enters the flash tower 2 in the form of make-up water.
However, excessive depressurization is not required by using the second depressurization valve 7, a part of water vapor is already contained in the steam-water mixture in the second depressurization valve 7, but the amount of the part of water vapor may not be enough to be used as the supplementing water, so that the second depressurization valve 7 is adjusted according to the actual situation, if the water lost in the carbon capturing process can be completely supplemented without depressurization, the valve of the second depressurization valve 7 is fully opened, no pressure loss exists after the steam-water mixture passes through the valve, if the water vapor in the steam-water mixture is not enough to be used as the supplementing water without depressurization, the depressurization is properly performed to increase the content of the water vapor in the steam-water mixture, and the required water vapor amount can be met without performing too much pressure drop, so that the temperature of the steam-water mixture after depressurization is not reduced too much, and a large heat utilization space exists for the part of low-grade heat.
The rest liquid water in the third gas-liquid separator 12 enters the hot side of the second reboiler 5 to be heated and resolved for the MEA/MDEA rich liquid entering the cold side of the second reboiler 5, thereby resolving more CO 2 The gas and the liquid water after heat exchange are introduced into a boiler 17.
In some embodiments, the low pressure water vapor heat exchange system further comprises a water vapor recovery system that self-recovers water vapor in the second capture system. The water vapor recovery system is a passage formed by a gas output port of the second gas-liquid separator 11, a gas compressor 15 and a water vapor inlet of the regeneration tower 3 which are connected in sequence.
Specifically, as shown in fig. 3: the MEA/MDEA lean solution is decompressed by a first decompression valve 9 and is compressed by a compressor 15 by a second gas-liquid separator 11, so that the water vapor in the MEA/MDEA lean solution is matched with the regeneration pressure of the regeneration tower 3 and is sent back to the regeneration tower 3 again. The flow control of the water vapor can be realized by controlling the pressure of the output end of the first pressure reducing valve 9, the water vapor can be liquefied and released to change the heat after entering the regeneration tower 3, and finally the water vapor enters the regeneration tower 3 in the form of supplementing water, so that on one hand, the heat of the water vapor in the MEA/MDEA lean solution is recovered, and on the other hand, the temperature of the MEA/MDEA lean solution is reduced by reducing the pressure, so that the MEA/MDEA lean solution can fully absorb the heat in the subsequent heat exchange process.
As shown in FIG. 4, the present embodiment proposes to intensify CO using the above device 2 The regeneration process method comprises the following steps:
capturing alcohol amine solution absorbs CO in raw material gas in absorption tower 1 2 Obtaining alcohol amine rich liquid;
after preliminary analysis of the alcohol amine rich solution in the flash tower 2, a part of MEA/MDEA rich solution with the volume percentage of 9-12% enters a second reboiler 5 for heating analysis, and the analyzed CO 2 Introducing into a flash tower 2; the MEA/MDEA semi-rich liquid with the temperature of 90-100 ℃ after being resolved by the flash tower 2 is mixed with the rest of the alcohol amine rich liquid which is heated for pressurization, and then enters a regeneration tower 3 for resolving;
the MEA/MDEA semi-rich liquid analyzed by the regeneration tower 3 enters a first reboiler 4 to be heated and analyzed, and the analyzed CO 2 Introducing into a regeneration tower 3, and resolving CO with the regeneration tower 3 2 Jointly introducing the two materials into a flash tower 2; CO 2 And collecting and storing the heat in the flash tower 2 after heat exchange.
The MEA/MDEA lean solution analyzed by the first reboiler 4 is decompressed and then subjected to heat exchange and circulated to the absorption tower 1.
Preferably, the resolution temperature of reboiler 2 is 90-110deg.C, preferably 100deg.C; the pressure is 0.8-1.5bar, preferably 1bar; the resolving temperature of the second water vapor heat exchange system is 115-130 ℃, preferably 120 ℃; the pressure is 2-3bar, preferably 2.5bar; the resolving temperature of the regeneration tower 3 is 115-130 ℃, preferably 120 ℃; the pressure is 2-3bar, preferably 2.5bar; the resolving temperature of the first water vapor heat exchange system is 90-110 ℃, preferably 100 ℃; the pressure is 0.8-1.5bar, preferably 1bar.
Illustratively: adsorption of CO in feed gas using MEA/MDEA solution 2 Wherein the device in this embodiment is adapted for CO 2 5% -25% of feed gas. The raw material gas in the embodiment can be power plant flue gas, and is specific; absorption of CO in feed gas via MEA/MDEA solution 2 The gas, clean flue gas is discharged through the gas outlet of the absorption tower 1, and CO 2 The gas is dissolved in MEA/MDEA solution, the MEA/MDEA rich solution is pressurized by a first rich solution pump 13 and then enters a flash tower 2, and the solution is controlled by adjusting the flash pressureAnalysis progress, CO resolved in flash column 2 2 The volume percentage is total resolved CO 2 The volume of the steam turbine is 5-7%, so that the steam extraction amount of the steam turbine can be reduced by reasonably utilizing low-grade heat of the steam, more high-grade steam is prevented from being pumped, 2-3% of high-grade steam can be saved, and the purpose of reducing energy loss of a power plant is achieved.
The MEA/MDEA solution rich solution after being resolved by the flash tower 2 enters the cold side of the second reboiler 5 with the volume percentage of 9-12%; the low-pressure steam on the hot side of the second reboiler 5 is utilized for analysis, the MEA/MDEA solution rich solution is changed into MEA/MDEA semi-rich solution after being analyzed, and the MEA/MDEA semi-rich solution is introduced into a first gas-liquid separator 10 for gas-liquid separation, wherein the separated CO 2 The gas is introduced into a flash tower 2, and the separated MEA/MDEA semi-rich liquid is introduced into the cold side output end of a lean-rich liquid heat exchanger 6.
It can be understood that a part of the MEA/MDEA rich liquid after being resolved by the flash tower 2 enters the cold side of the second steam heat exchange system (the cold side of the second reboiler 5) to form MEA/MDEA semi-rich liquid, and the other rest of the MEA/MDEA rich liquid enters the cold side of the lean-rich liquid heat exchanger 6, exchanges heat with the MEA/MDEA lean liquid entering the hot side of the lean-rich liquid heat exchanger 6, flows out from the cold side output end of the lean-rich liquid heat exchanger 6 and is converged with the MEA/MDEA semi-rich liquid, and can be introduced into the regeneration tower 3 after pressurizing the mixed liquid by arranging the second rich liquid pump 14.
The MEA/MDEA semi-rich liquid flows out of the regeneration tower 3 and enters the cold side of the first reboiler 4, and CO in the MEA/MDEA semi-rich liquid is heated 2 The gas escapes into the regeneration tower 3 for enrichment, the MEA/MDEA semi-rich liquid is changed into MEA/MDEA lean liquid, the MEA/MDEA lean liquid is depressurized to be near 1bar through a first depressurization valve 9, and then the gas is subjected to heat exchange and circulated to the absorption tower 1.
In this embodiment, the first trapping system and the second trapping system are used to perform CO in the alcohol amine rich solution 2 The primary analysis of the water vapor is realized, and the first water vapor heat exchange system and the second water vapor heat exchange system assist in analysis, so that the utilization of low-grade heat of water vapor can be increased, the high-grade water vapor can be less pumped for carbon capture, the power generation efficiency of a power plant is improved, the energy consumption is reduced by 10% -20%, and the dioxide is simultaneously realizedThe carbon removal rate reaches 95 percent.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
For purposes of this disclosure, the terms "one embodiment," "some embodiments," "example," "a particular example," or "some examples," etc., 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 invention. In this specification, schematic representations of the above terms are not necessarily directed 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, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (7)
1. CO (carbon monoxide) 2 A reproduction apparatus, comprising:
CO 2 double tower capture system, said CO 2 The double-tower trapping system comprises a circulating passage composed of a first trapping system and a second trapping system, wherein the first trapping system comprises a passage composed of an absorption tower, a flash tower and a cold side of a lean-rich liquid heat exchanger which are sequentially connected, and a passage composed of the flash tower, the cold side of a second reboiler, a first gas-liquid separator and an output end of the cold side of the lean-rich liquid heat exchanger which are sequentially connected, and is used for introducing a trapping alcohol amine solution to absorb CO in raw gas 2 ；
The second trapping system comprises a passage formed by an output end of a cold side of the lean-rich liquid heat exchanger, a regeneration tower, a cold side of a first reboiler, a hot side of the lean-rich liquid heat exchanger and a liquid inlet end of the absorption tower, which are sequentially connected, and is used for absorbing CO by utilizing the trapping alcohol amine solution in the first trapping system 2 Analyzing;
CO 2 recovery system of the CO 2 The recovery system recovers CO 2 Analytic CO that produces of double tower entrapment system 2 Storing after enrichment and recovery; and
the low-pressure steam heat exchange system comprises a first steam heat exchange system which takes low-pressure steam as a heat medium, wherein the first steam heat exchange system comprises a passage formed by a hot side of the first reboiler, a second pressure reducing valve, a third gas-liquid separator and a third air inlet of the flash tower which are connected in sequence; the low-pressure water vapor is depressurized by the second depressurization valve and then enters the third gas-liquid separator, and the separated water vapor is introduced into the flash tower to heat the trapped alcohol amine solution therein and supplement water.
2. The apparatus of claim 1, wherein the CO 2 The recovery system comprises a passage which is formed by a gas output port of the regeneration tower, a first air inlet of the flash evaporation tower, a gas output port of the flash evaporation tower and a storage device which are sequentially connected.
3. The apparatus of claim 1, wherein the CO 2 The recovery system comprises a recovery passage consisting of a gas output port of the first gas-liquid separator and a second gas inlet of the flash tower.
4. The apparatus of claim 1, wherein the CO 2 The recovery system comprises a recovery passage consisting of a gas output port of the first reboiler and a gas input port of the regeneration tower; wherein the input end of the cold side of the first reboiler is connected with the liquid outlet of the regeneration tower.
5. The apparatus of claim 1, wherein the low pressure steam heat exchange system further comprises a second steam heat exchange system, wherein the second steam heat exchange system comprises a passage comprised of a hot side of a second reboiler and a boiler; wherein the gas output port of the third gas-liquid separator is connected with the third gas inlet of the flash tower; and the hot side input end of the second reboiler is connected with the liquid outlet of the third gas-liquid separator.
6. Intensified CO 2 The regeneration process is characterized in thatThus, CO is enhanced by the device according to claim 5 2 Regeneration, comprising the steps of:
capturing CO in alcohol amine solution absorbing raw material gas 2 Obtaining alcohol amine rich liquid;
after preliminary analysis of the alcohol amine rich solution in the flash tower, the alcohol amine rich solution with the volume percentage of 9-12% enters a second reboiler for heating and analysis to generate CO 2 And alcohol amine semi-rich liquid, CO 2 Introducing the alcohol amine semi-rich liquid and the rest of the heated alcohol amine rich liquid into the flash tower, mixing and pressurizing, and then, introducing the mixture into a regeneration tower for deep analysis;
the alcohol amine semi-rich liquid after deep analysis of the regeneration tower enters a first reboiler to be heated and analyzed to generate CO 2 And alcohol amine lean solution, CO 2 Introducing the CO into the regeneration tower and resolving the CO with the regeneration tower 2 Introducing the mixture into the flash tower for heat exchange, and performing CO (carbon monoxide) after heat exchange 2 Collecting and storing;
and the alcohol amine lean solution is decompressed and then subjected to heat exchange and circulated to the absorption tower.
7. The method according to claim 6, wherein the alcohol amine rich liquid is controlled to have a resolution temperature of 90-110 ℃ and a pressure of 0.8-1.5bar in the flash tower; the resolving temperature of the second water vapor heat exchange system is 115-130 ℃ and the pressure is 2-3bar; the resolving temperature of the regeneration tower is 115-130 ℃ and the pressure is 2-3bar; the resolving temperature of the first water vapor heat exchange system is 90-110 ℃, and the pressure is 0.8-1.5bar.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101816878A (en) * | 2010-04-30 | 2010-09-01 | 四川省精细化工研究设计院 | Novel high-efficient compound decarbonization solvent |
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
| CN103357250A (en) * | 2012-04-06 | 2013-10-23 | 李志远 | Facility and process for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| EP2892631A2 (en) * | 2012-09-07 | 2015-07-15 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
| CN104826472A (en) * | 2015-04-23 | 2015-08-12 | 中石化石油工程设计有限公司 | Flue gas carbon dioxide capture recovery system |
| CN111054187A (en) * | 2019-12-18 | 2020-04-24 | 国家能源投资集团有限责任公司 | Recovery system and gas recovery method |
| CN113144836A (en) * | 2021-05-20 | 2021-07-23 | 中国华电科工集团有限公司 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7632476B2 (en) * | 2006-03-09 | 2009-12-15 | Praxair Technology, Inc. | Method of recovering carbon dioxide from a synthesis gas stream |
| JP5686987B2 (en) * | 2010-04-20 | 2015-03-18 | 三菱日立パワーシステムズ株式会社 | Exhaust gas treatment system equipped with carbon dioxide chemical absorption equipment |
| US9314732B2 (en) * | 2013-01-09 | 2016-04-19 | Fluor Technologies Corporation | Systems and methods for reducing the energy requirements of a carbon dioxide capture plant |
| JP6157925B2 (en) * | 2013-05-20 | 2017-07-05 | 株式会社東芝 | Carbon dioxide separation and recovery device and operation method thereof |
-
2022
- 2022-03-17 CN CN202210268006.1A patent/CN114712990B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101816878A (en) * | 2010-04-30 | 2010-09-01 | 四川省精细化工研究设计院 | Novel high-efficient compound decarbonization solvent |
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
| CN103357250A (en) * | 2012-04-06 | 2013-10-23 | 李志远 | Facility and process for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
| EP2892631A2 (en) * | 2012-09-07 | 2015-07-15 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| CN104826472A (en) * | 2015-04-23 | 2015-08-12 | 中石化石油工程设计有限公司 | Flue gas carbon dioxide capture recovery system |
| CN111054187A (en) * | 2019-12-18 | 2020-04-24 | 国家能源投资集团有限责任公司 | Recovery system and gas recovery method |
| CN113144836A (en) * | 2021-05-20 | 2021-07-23 | 中国华电科工集团有限公司 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
Non-Patent Citations (1)
| Title |
|---|
| 烟气CO_2捕集热能梯级利用节能工艺耦合优化;陆诗建;高丽娟;王家凤;赵东亚;王鑫;朱全民;;化工进展(02);全文 * |
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