CN110013740B - Device for absorbing and capturing carbon dioxide by amine method - Google Patents
Device for absorbing and capturing carbon dioxide by amine method Download PDFInfo
- Publication number
- CN110013740B CN110013740B CN201910257422.XA CN201910257422A CN110013740B CN 110013740 B CN110013740 B CN 110013740B CN 201910257422 A CN201910257422 A CN 201910257422A CN 110013740 B CN110013740 B CN 110013740B
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- outlet
- liquid
- inlet
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 184
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 92
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 37
- 150000001412 amines Chemical class 0.000 title claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 176
- 238000003795 desorption Methods 0.000 claims abstract description 77
- 238000010521 absorption reaction Methods 0.000 claims abstract description 76
- 230000007246 mechanism Effects 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 57
- 239000003546 flue gas Substances 0.000 claims description 57
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 53
- 238000001816 cooling Methods 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000002250 absorbent Substances 0.000 description 14
- 230000002745 absorbent Effects 0.000 description 14
- 238000010438 heat treatment Methods 0.000 description 12
- 230000008929 regeneration Effects 0.000 description 11
- 238000011069 regeneration method Methods 0.000 description 11
- 239000000498 cooling water Substances 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000012264 purified product Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- -1 alcohol amine Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000011064 split stream procedure Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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
-
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D2252/204—Amines
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of carbon dioxide absorption equipment, and provides an amine method carbon dioxide absorption and capture device, which comprises an absorption tower, a desorption tower, an exhaust channel communicated with the desorption tower, an air inlet channel and an air outlet channel respectively communicated with the absorption tower, a reboiler for providing heat for the desorption tower, a lean solution channel respectively communicated with the absorption tower and the desorption tower, and a rich solution channel respectively communicated with the absorption tower and the desorption tower; the device for absorbing and capturing carbon dioxide by the amine method further comprises a heat recovery mechanism for recovering residual heat left in the desorption tower when the carbon dioxide is released and transmitting the residual heat into the rich liquid channel. Residual heat is remained in the carbon dioxide released by the desorption tower, and is conducted into the lean solution channel after being recovered by the heat recovery mechanism, so that the rich solution in the rich solution channel is heated, and the heated rich solution enters the desorption tower to reduce the energy consumption of the desorption tower.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide absorption equipment, and particularly relates to a device for absorbing and capturing carbon dioxide by an amine method.
Background
The carbon dioxide discharged by a large amount of fossil fuels is a main cause of global warming, and the capture and utilization and the sequestration of the discharged carbon dioxide are important measures for coping with climate change. At present, carbon dioxide is captured mainly by adopting a chemical absorption method carbon capture technology after fossil fuel is combusted, and an adopted absorbent is an organic amine solution (organic amine can be selected as alcohol amine).
The conventional organic amine carbon capturing system (note: in the present application, the lean liquid and the rich liquid are mainly the same absorbent; carbon dioxide absorbed in the lean liquid is lower than carbon dioxide absorbed in the rich liquid) is generally composed of an absorption tower, a desorption tower, a reboiler (the reboiler conducts heat in the external hot steam into the desorption tower and discharges the cooled external hot steam as liquid water), and the like. The flue gas (containing CO 2) enters from the lower part of the absorption tower, reversely contacts with the absorbent (lean solution) sprayed from the tower top in the tower (reverse contact: the flue gas moves from bottom to top in the absorption tower, the absorbent sprays from top to bottom in the absorption tower), and the flue gas with CO2 removed is discharged from the upper part of the absorption tower. And the absorbent liquid (rich liquid) absorbing the carbon dioxide is pumped into the absorption tower by the rich liquid pump and then is sent into the desorption tower for regeneration (regeneration: releasing the carbon dioxide in the rich liquid), and the released carbon dioxide gas flow is condensed by the condenser and then is output. And hot lean solution at the bottom of the desorption tower is sprayed from the top of the absorption tower under the action of a lean solution pump, so that the circulation of the system is realized. Although the carbon capture system can capture carbon dioxide in the flue gas, a large amount of waste heat is wasted in the regeneration process of the desorber, so that the energy consumption is too much, and the popularization and the application of the technology are not facilitated.
Disclosure of Invention
The invention aims to provide a device for absorbing and capturing carbon dioxide by an amine method, which aims to solve the technical problem that a large amount of waste heat is wasted in the regeneration process of a desorption tower in the prior art, so that too much energy is consumed.
In order to achieve the above purpose, the invention adopts the following technical scheme: the device for absorbing and capturing carbon dioxide by an amine method comprises an absorption tower, a desorption tower, an exhaust channel communicated with the desorption tower, an air inlet channel and an air outlet channel which are respectively communicated with the absorption tower, a reboiler for providing heat for the desorption tower, a lean solution channel which is respectively communicated with the absorption tower and the desorption tower, and a rich solution channel which is respectively communicated with the absorption tower and the desorption tower; the device for absorbing and capturing carbon dioxide by the amine method further comprises a heat recovery mechanism for recovering residual heat left in the desorption tower when carbon dioxide is released and transmitting the residual heat into the rich liquid channel.
Further, the heat recovery mechanism includes a first heat exchanger, and the lean liquid passage exchanges heat with the rich liquid passage through the first heat exchanger.
Further, the heat recovery mechanism further includes a second heat exchanger and a flash tank provided on the lean liquid passage; the flash tank has a vapor passage in communication with the desorber; the steam passage exchanges heat with the rich liquid passage through the second heat exchanger.
Further, a vapor compressor is also provided on the vapor passage upstream of the second heat exchanger.
Further, the system also comprises a third heat exchanger, and the rich liquid channel exchanges heat with the water outlet pipe of the reboiler through the third heat exchanger.
Further, the exhaust passage is provided with a fourth heat exchanger, and the exhaust passage exchanges heat with the rich liquid passage through the fourth heat exchanger.
Further, the device also comprises a fifth heat exchanger, wherein a gas compressor is arranged on the exhaust passage, and the exhaust passage downstream of the gas compressor exchanges heat with the rich liquid passage through the fifth heat exchanger.
Further, the absorption tower further comprises a tower-stage cooler for cooling absorption liquid, and a liquid inlet and a liquid outlet of the tower-stage cooler are respectively communicated with the absorption tower.
Further, the device also comprises a flue gas pretreatment tower for spraying alkali liquor, wherein a first flue gas inlet is formed in the bottom of the flue gas pretreatment tower, a first flue gas outlet is formed in the top of the flue gas pretreatment tower, and the first flue gas outlet is communicated with the air inlet channel.
Further, the flue gas water scrubber for spraying water is further comprised, a second flue gas inlet is arranged at the bottom of the flue gas water scrubber, a second flue gas outlet communicated with the external space is arranged at the top of the flue gas water scrubber, and the second flue gas inlet is communicated with the exhaust channel.
The device for absorbing and capturing carbon dioxide by the amine method has the beneficial effects that: compared with the prior art, the device for absorbing and capturing carbon dioxide by the amine method provided by the invention has the advantages that the flue gas enters the absorption tower from the air inlet channel, and the carbon dioxide in the flue gas is discharged from the air outlet channel after being absorbed by lean liquid in the absorption tower; the lean solution absorbing carbon dioxide in the absorption tower is changed into rich solution and is conveyed to the desorption tower along a rich solution channel, carbon dioxide in the rich solution in the desorption tower is discharged from an exhaust channel after being released, and a reboiler supplies heat for the desorption tower so that the carbon dioxide in the rich solution in the desorption tower can be released; the rich liquid released with carbon dioxide in the desorption tower is changed into lean liquid and then is conveyed into the absorption tower along a lean liquid channel; residual heat is remained in the carbon dioxide released by the desorption tower, and is conducted into the lean solution channel after being recovered by the heat recovery mechanism, so that the rich solution in the rich solution channel is heated, and the heated rich solution enters the desorption tower to reduce the energy consumption of the desorption tower.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of an apparatus for absorbing and capturing carbon dioxide by an amine method according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a device for absorbing and capturing carbon dioxide by an amine method according to a second embodiment of the present invention;
FIG. 3 is a schematic diagram of a device for absorbing and capturing carbon dioxide by an amine method according to an embodiment of the present invention;
Fig. 4 is a schematic structural diagram of an apparatus for absorbing and capturing carbon dioxide by an amine method according to an embodiment of the present invention.
Wherein, each reference sign in the figure:
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
It will be understood that when an element is referred to as being "mounted" or "disposed" on another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element.
It is to be understood that the terms "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are merely for convenience in describing and simplifying the description based on the orientation or positional relationship shown in the drawings, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus are not to be construed as limiting the invention.
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 one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In addition, "high temperature" and "low temperature" refer to the designations before and after heating of the liquid, and it is understood that, for example: the liquid before heating is referred to as low-temperature liquid, and the liquid after heating is referred to as high-temperature liquid, with respect to the same heating apparatus.
Alternatively, "high temperature" refers to a temperature greater than or equal to 100 degrees celsius and "low temperature" refers to a temperature less than 100 degrees celsius.
In addition, "cold" is understood to mean normal temperature. Such as; the cold water is water at normal temperature. "hot" is understood to mean a temperature exceeding ambient temperature. Specifically, alternatively, the normal temperature is 25 ℃.
In the present application, in the heat exchange device, the side through which the heat source (heat source: such as hot water) passes is the hot side, and the side through which the heated substance passes is the cold side; the heat source enters from the inlet of the hot side and exits from the outlet of the hot side; the heated material enters from the inlet of the cold side and exits from the outlet of the cold side.
Referring to fig. 1, an apparatus for absorbing and capturing carbon dioxide by an amine method according to the present invention will now be described. The device for absorbing and capturing carbon dioxide by the amine method comprises an absorption tower 10, a desorption tower 11, an exhaust channel T1 communicated with the desorption tower 11, an air inlet channel T21 and an air outlet channel T22 respectively communicated with the absorption tower 10, a reboiler 23 for providing heat for the desorption tower 11, a lean solution channel T31 respectively communicated with the absorption tower 10 and the desorption tower 11, and a rich solution channel T32 respectively communicated with the absorption tower 10 and the desorption tower 11; the apparatus for capturing carbon dioxide by the amine method further includes a heat recovery mechanism (not shown) for recovering the residual heat left in the desorption tower 11 at the time of releasing carbon dioxide and conducting the residual heat into the rich liquid passage T32.
In this way, the flue gas enters the absorption tower 10 from the air inlet channel T21, and carbon dioxide in the flue gas is absorbed by lean liquid in the absorption tower 10 and then is discharged from the air outlet channel T22; the lean liquid having absorbed carbon dioxide in the absorption tower 10 becomes rich liquid and is transported to the desorption tower 11 along the rich liquid channel T32, carbon dioxide in the rich liquid in the desorption tower 11 is released and then discharged from the exhaust channel T1, and the reboiler 23 supplies heat to the desorption tower 11 so that carbon dioxide in the rich liquid in the desorption tower 11 can be released; the rich liquid in which carbon dioxide is released in the desorption tower 11 becomes lean liquid and is then sent to the absorption tower 10 along a lean liquid channel T31; the desorber 11 releases residual heat in the carbon dioxide, and the residual heat is recovered by the heat recovery mechanism and is transferred into the lean solution channel T31, so that the rich solution in the rich solution channel T32 is heated, and the heated rich solution enters the desorber 11 to reduce the energy consumption of the desorber 11.
There are various forms of the waste heat, and some are contained in the discharged liquid (such as the lean liquid), some are contained in the discharged gas (such as the discharged carbon dioxide gas), and some are also contained elsewhere in the desorption column 11, as long as the waste heat can be recovered and conducted into the rich liquid passage T32, which is not limited only.
Alternatively, in one embodiment, the lean liquid passage T31 is in a pipe shape. Specifically, in one embodiment, the lean solution passage T31 is a circular tube. Specifically, in one embodiment, the lean solution passage T31 has therein a pump body for driving the movement of the liquid/gas in the lean solution passage T31.
Alternatively, in one embodiment, the rich liquid passage T32 is in a pipe shape. Specifically, in one embodiment, the rich liquid passage T32 is a circular tube. Specifically, in one embodiment, the rich liquid passage T32 has therein a pump body for driving the movement of the liquid/gas in the rich liquid passage T32.
Alternatively, in one embodiment, the intake passage T21 is in a pipe shape. Specifically, in one embodiment, the intake passage T21 is a circular tube. Specifically, in one embodiment, the intake passage T21 has therein a pump body for driving the movement of liquid/gas in the intake passage T21.
Alternatively, in one embodiment, the outlet channel T22 is in the form of a pipe. Specifically, in one embodiment, the air outlet channel T22 is a circular tube. Specifically, in one embodiment, the outlet channel T22 has a pump body therein for driving the movement of the liquid/gas in the outlet channel T22.
Further, referring to fig. 1, as a specific embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the invention, the heat recovery mechanism includes a first heat exchanger 19, and the lean solution channel T31 exchanges heat with the rich solution channel T32 through the first heat exchanger 19. In this way, the lean liquid itself remains with heat after being output from the desorption tower 11, and this part of heat is conducted to the rich liquid passage T32 through the first heat exchanger 19 to raise the lean liquid temperature in the rich liquid passage T32.
Alternatively, in one embodiment, the first heat exchanger 19 is a dividing wall heat exchanger. Specifically, in one embodiment, the first heat exchanger 19 is any one of a plate heat exchanger, a jacket heat exchanger, an immersed coil type, a shower type heat exchanger, a double pipe heat exchanger, and a shell-and-tube heat exchanger.
Further, referring to fig. 1, as an embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the present invention, the heat recovery mechanism further includes a second heat exchanger 20 and a flash tank 24 disposed on the lean liquid channel T31; the flash tank 24 has a vapor passage T4 communicating with the desorption column 11; the steam passage T4 exchanges heat with the rich liquid passage T32 through the second heat exchanger 20. As such, after the lean liquid in the lean liquid passage T31 passes through the flash tank 24, the liquid generated in the flash tank 24 continues to flow along the lean liquid passage T31, the gas portion generated in the flash tank 24 is transported along the steam passage T4, and the heat of the steam in the steam passage T4 is conducted into the rich liquid in the rich liquid passage T32 through the second heat exchanger 20 to heat the rich liquid in the rich liquid passage T32.
Alternatively, in one embodiment, the steam channel T4 is in the form of a pipe. Specifically, in one embodiment, the steam channel T4 is a circular tube. Specifically, in one embodiment, the vapor channel T4 has a pump body therein for driving the movement of liquid/gas within the vapor channel T4.
Alternatively, in one embodiment, the second heat exchanger 20 is a dividing wall heat exchanger. Specifically, in one embodiment, the second heat exchanger 20 is any one of a plate heat exchanger, a jacket heat exchanger, an immersed coil type, a shower type heat exchanger, a double pipe heat exchanger, and a shell and tube heat exchanger.
Further, referring to fig. 1, as a specific embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the present invention, a vapor compressor 25 is further disposed on the vapor channel T4 upstream of the second heat exchanger 20. In this manner, the vapor compressor 25 can raise the temperature in the vapor passage T4 so that the vapor passage T4 transfers more heat into the lean liquid passage T31 through the second heat exchanger 20; in addition, the vapor compressor 25 can raise the pressure in the vapor passage T4, so that the pressure of the vapor in the desorption tower 11 is more balanced when entering the desorption tower 11, thereby being beneficial to protecting the desorption tower 11.
Further, referring to fig. 1, as a specific embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the present invention, the device for absorbing and capturing carbon dioxide by an amine method further includes a third heat exchanger 21, and the rich liquid channel T32 exchanges heat with the water outlet pipe T5 of the reboiler 23 through the third heat exchanger 21. In this way, the heat in the hot water discharged from the water outlet pipe T5 in the reboiler 23 is transferred to the rich liquid passage T32 through the third heat exchanger 21, and the heat in the wastewater from the water outlet pipe T5 is reused.
Alternatively, in one embodiment, the outlet pipe T5 is in the form of a pipe. Specifically, in one embodiment, the water outlet pipe T5 is a circular pipe. Specifically, in one embodiment, the outlet tube T5 has a pump body therein for driving the movement of liquid/gas in the outlet tube T5.
Alternatively, in one embodiment, the third heat exchanger 21 is a dividing wall heat exchanger. Specifically, in one embodiment, the third heat exchanger 21 is any one of a plate heat exchanger, a jacket heat exchanger, an immersed coil type, a shower type heat exchanger, a double pipe heat exchanger, and a shell-and-tube heat exchanger.
Specifically, referring to fig. 2, in one embodiment, high temperature steam S16 enters reboiler 23 from the hot side inlet of reboiler 23, heat is transferred to reheated lean solution S15 entering from the cold side inlet of reboiler 23 through phase change, and reheated lean solution S15 is heated and then injected into desorber 11 from the cold side outlet again to increase the heat required for carbon dioxide regeneration. The high-temperature steam S16 is condensed into high-temperature water S17 in the reboiler 23 and discharged from a hot side outlet of the reboiler 23. The hot rich liquid S9 is desorbed and regenerated to form hot lean liquid S10, the hot lean liquid S10 is discharged from the bottom outlet of the desorption tower 11, enters the flash tank 24 through the inlet of the flash tank 24, and the generated flash steam S12 and medium Wen Pinye S11 are respectively discharged from the top outlet and bottom outlet of the flash tank 24. The flash steam S12 enters the vapor compressor 25 from the inlet of the vapor compressor 25, is compressed to be compressed steam S13 of high temperature and high pressure, and is discharged. The compressed steam S13 enters the second heat exchanger 20 from the hot side inlet of the second heat exchanger 20, and is cooled down to become saturated steam S14. Saturated steam S14 then enters the desorber 11 from the bottom gas inlet of the desorber 11 for heating.
Optionally, referring to fig. 3, in an embodiment, the high-temperature water S17 enters the third heat exchanger 21 from the hot side inlet of the third heat exchanger 21, and after being cooled by heat exchange, the high-temperature water S17 becomes cold return water S31, and is discharged from the hot side outlet back to the heating pipe network system.
Further, referring to fig. 1, as a specific embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the present invention, the device for absorbing and capturing carbon dioxide by an amine method further includes a fourth heat exchanger 22, and the exhaust passage T1 exchanges heat with the rich liquid passage T32 through the fourth heat exchanger 22. In this way, the carbon dioxide gas and the water vapor discharged from the exhaust passage T1 carry heat, and the heat is transferred into the rich liquid passage T32 through the fourth heat exchanger 22.
Alternatively, in one embodiment, fourth heat exchanger 22 is a dividing wall heat exchanger. Specifically, in one embodiment, the fourth heat exchanger 22 is any one of a plate heat exchanger, a jacketed heat exchanger, an immersed serpentine heat exchanger, a spray heat exchanger, a double pipe heat exchanger, and a shell and tube heat exchanger.
Alternatively, referring to fig. 4, in one embodiment, the initial rich liquid S4 is split into two split first rich liquid split S8 and second rich liquid split S18, wherein the second rich liquid split S18 enters the fourth heat exchanger 22 from the cold side inlet of the fourth heat exchanger 22, the second rich liquid split S18 is discharged from the cold side outlet into the desorption tower 11 after recovering latent heat of water vapor in the initial product gas S19 generated in the desorption tower 11, and the initial product gas S19 enters the carbon dioxide water scrubber 28 after being cooled in the fourth heat exchanger 22. The heat load of the reboiler 23 can be further reduced by recovering the steam heat in the initial product gas S19 in the fourth heat exchanger 22 by the second rich split S18, thereby reducing the energy consumption for system regeneration.
Alternatively, referring to fig. 4, in one embodiment, the hot side inlet and outlet of the fourth heat exchanger 22 are connected to the top gas outlet of the desorber 11 and the bottom inlet of the carbon dioxide scrubber 28, respectively, and the cold side inlet and outlet of the fourth heat exchanger 22 are connected to the outlet of the rich liquid pump 18 and the top liquid inlet of the desorber 11, respectively.
Further, referring to fig. 1, as a specific embodiment of the device for absorbing and capturing carbon dioxide by an amine method provided by the present invention, the device for absorbing and capturing carbon dioxide by an amine method further includes a fifth heat exchanger 29, a gas compressor 32 is disposed on the exhaust passage T1, and the exhaust passage T1 downstream of the gas compressor 32 exchanges heat with the rich liquid passage T32 through the fifth heat exchanger 29. In this way, the gas compressor 32 is convenient to store when compressing the gas (carbon dioxide) in the exhaust passage T1, and a large amount of heat is generated during compression and transferred to the rich liquid passage T32 through the fifth heat exchanger 29.
Optionally, in one embodiment, fifth heat exchanger 29 is a dividing wall heat exchanger. Specifically, in one embodiment, the fifth heat exchanger 29 is any one of a plate heat exchanger, a jacket heat exchanger, an immersed coil type, a shower type heat exchanger, a double pipe heat exchanger, and a shell-and-tube heat exchanger.
Alternatively, referring to FIG. 4, in one embodiment, the cold side inlet and outlet of the fifth heat exchanger 29 are connected to the cold side outlet of the fourth heat exchanger 22 and the second stage liquid inlet of the desorber 11, respectively, and the hot side inlet and outlet of the fifth heat exchanger 29 are connected to the gas cooler 33, the first carbon dioxide cooler 35, the second carbon dioxide cooler 37 outlet and the cooling water cooler 40 inlet, respectively. The outlet of the cooling water cooler 40 is connected with the inlet of the gas cooler 33, the first carbon dioxide cooler 35 and the second carbon dioxide cooler 37; specifically, the second rich liquid split stream S18 is discharged from the cold side outlet after heat exchange and temperature rise by the fourth heat exchanger 22, enters the fifth heat exchanger 29 through the cold side inlet of the fifth heat exchanger 29, and is discharged from the cold side outlet into the second tower stage liquid inlet of the desorption tower 11 after temperature rise. The carbon dioxide cooling water S28 is fed from the inlets of the gas cooler 33, the first carbon dioxide cooler 35, and the second carbon dioxide cooler 37 to the corresponding coolers, and the high-temperature heat of the compressed carbon dioxide is recovered as high-temperature cooling water S29. The high-temperature cooling water S29 enters the fifth heat exchanger 29 from the hot side inlet of the fifth heat exchanger 29, is discharged from the hot side outlet of the fifth heat exchanger 29 after being cooled, and then enters the cooling water cooler 40 to be cooled further to become carbon dioxide cooling water S28. By providing the fifth heat exchanger 29 to use the heat generated during compression of carbon dioxide for rich liquid regeneration, the heat supply duty of the reboiler 23 can be further reduced, thereby reducing the system regeneration energy consumption.
Alternatively, in one embodiment, the initial product gas S19 produced by regeneration of the hot rich liquid S9 in the desorber 11 is withdrawn from the top gas outlet of the desorber and fed to the carbon dioxide water scrubber 28 via the bottom gas inlet thereof. The initial product gas S19 contains a small amount of volatile absorbent components which are removed in the carbon dioxide water scrubber 28 to become the purified product gas S20. The purified product gas S20 is cooled by the condenser 30 and then enters the gas-liquid separator 31, the obtained condensed water S21 is refluxed to the carbon dioxide water scrubber 28 as washing water, and the recovered water S22 having absorbed the volatilized absorbent component flows out from the bottom liquid outlet of the water scrubber and is subjected to the desorption column 11 through the top liquid inlet of the desorption column 11.
Specifically, in one embodiment, the carbon dioxide gas S23 discharged from the top outlet of the gas-liquid separator 31 enters the gas compressor 32 to be compressed, and is then cooled by the gas cooler 33, thus obtaining liquid carbon dioxide S24 through successive three-stage compression cooling.
Alternatively, in one embodiment, the absorbent make-up solution S25 required for the operation of the system is injected into the absorbent storage tank 27 through the inlet of the absorbent storage tank 27, and the lean solution S30 after regeneration and cooling is delivered from the bottom outlet of the absorbent storage tank 27 to the absorbent cooler 15 through the absorbent pump 41 for cooling and then injected into the absorption tower 10.
Further, referring to fig. 1, as a specific embodiment of the device for capturing carbon dioxide by absorption with an amine method provided by the invention, a tower stage cooler 14 for cooling an absorption liquid is further included, and a liquid inlet and a liquid outlet of the tower stage cooler 14 are respectively communicated with the absorption tower 10. In this way, the lean liquid (or the intermediate lean liquid between the lean liquid and the rich liquid concentration) in the absorption tower 10 is refluxed into the absorption tower 10 after being cooled by the tower stage cooler 14 (alternatively, the lean liquid refluxed into the absorption tower 10 is sprayed down from the top of the absorption tower 10), so that the temperature of the lean liquid in the absorption tower 10 is lowered, thereby increasing the absorption liquid load (absorption liquid load: the amount of carbon dioxide absorbed per unit of absorption liquid).
Alternatively, in one embodiment, the absorption liquid S3 entering the absorption column 10 reacts exothermically with carbon dioxide, and the heat generated will cause the absorption liquid to rise in temperature, which will reduce the amount of carbon dioxide absorbed by the absorption liquid, thus withdrawing the higher temperature semi-lean liquid S7 at the final stage of the absorption column 10, cooling it by the stage cooler 14, and re-injecting it into the absorption column. The initial rich liquid S4 after reaction is discharged from a liquid outlet at the bottom of the absorption tower 10, is conveyed by a rich liquid pump 18 to enter the heat exchanger from a cold side inlet of a first heat exchanger 19, is discharged from a cold side outlet of the first heat exchanger 19 after heating and heating, then enters the heat exchanger from a cold side inlet of a second heat exchanger 20, is discharged from a cold side outlet of the second heat exchanger 20 after heating and heating, enters the heat exchanger from a cold side inlet of a third heat exchanger 21, is discharged from a cold side outlet of the third heat exchanger 21 after heating and heating, and the obtained hot rich liquid S9 enters the desorption tower 11 from a second tower liquid inlet of the desorption tower 11 for carbon dioxide regeneration.
Optionally, in one embodiment, the medium Wen Pinye S11 (medium Wen Pinye S11: liquid output from flash tank 24) is fed from the hot side inlet of the first heat exchanger 19 to the first heat exchanger 19 by lean pump 26, cooled down and discharged from the hot side outlet of the first heat exchanger 19 to the absorption liquid storage tank 27.
Alternatively, in one embodiment, the inlet of the tower stage cooler 14 is connected to the final tower stage liquid outlet of the absorber tower 10, and the outlet of the tower stage cooler 14 is connected to the final tower stage liquid inlet of the absorber tower 10.
Further, referring to fig. 1, as a specific embodiment of the device for capturing carbon dioxide by absorption with an amine method provided by the invention, the device further comprises a flue gas pretreatment tower 12 for spraying alkali liquor, a first flue gas inlet (not shown) is formed in the bottom of the flue gas pretreatment tower 12, a first flue gas outlet (not shown) is formed in the top of the flue gas pretreatment tower 12, and the first flue gas outlet is communicated with an air inlet channel T21. In this way, before the flue gas enters the absorption tower 10 from the air inlet channel T21, alkali liquor is sprayed through the flue gas pretreatment tower 12 for removing pollutants such as sulfur oxides, nitrogen oxides and the like.
Alternatively, referring to FIG. 3, in one embodiment, the gas outlet of the flue gas pretreatment column 12 is connected to the gas inlet of the absorber column 10, the liquid outlet at the bottom of the flue gas pretreatment column 12 is connected to the inlet of the lye pump 38, the outlet of the lye pump 38 is connected to the inlet of the lye cooler 39, and the outlet of the lye cooler 39 is connected to the top inlet of the flue gas pretreatment column 12.
Optionally, referring to FIG. 4, in one embodiment, the initial flue gas S1 enters the flue gas pretreatment tower 12 from a bottom gas inlet thereof and reacts with the pretreatment lye S26 sprayed from the top of the tower to remove pollutants such as sulfur oxides and nitrogen oxides. The pretreated flue gas S2 enters the absorption tower 10 from a gas inlet at the bottom of the absorption tower and reacts with absorption liquid S3 sprayed from the top of the tower.
Further, referring to fig. 1, as a specific embodiment of the device for capturing carbon dioxide by absorption with an amine method provided by the invention, the device further comprises a flue gas water scrubber 13 for spraying water, a second flue gas inlet (not shown) is arranged at the bottom of the flue gas water scrubber 13, a second flue gas outlet (not shown) communicated with an external space is arranged at the top of the flue gas water scrubber 13, and a second flue gas inlet is communicated with the exhaust channel T1. In this way, the flue gas is cleaner after being sprayed and cleaned by the flue gas water scrubber 13, and the cleaned gas which is exhausted from the second flue gas outlet is delayed to be exhausted into the external environment, so that pollution is reduced.
Optionally, in one embodiment, the bottom gas inlet of the flue gas scrubber 13 is connected to the top gas outlet of the absorber 10, the bottom liquid outlet of the flue gas scrubber 13 is connected to the inlet of the scrubber water pump 16, the outlet of the scrubber water pump 16 is connected to the inlet of the scrubber water cooler 17, and the outlet of the scrubber water cooler 17 is connected to the top liquid inlet of the flue gas scrubber 13.
Optionally, in one embodiment, the decarbonized flue gas S5 is discharged from the top gas outlet of the absorption tower 10, enters the tower through the bottom gas inlet of the flue gas water scrubber 13, contacts with the water scrubber spray water S27 sprayed from the tower top, the volatile absorbent component entrained in the decarbonized flue gas S5 is absorbed by the washing water, and the obtained purified flue gas S6 is discharged from the top gas outlet of the washing tower and can be discharged into the atmosphere through a chimney.
Alternatively, in one embodiment, the absorber 10 liquid outlet is connected to the rich liquid pump 18 inlet, and the rich liquid pump 18 outlet is connected to the first heat exchanger 19 cold side inlet; the cold side outlet of the first heat exchanger 19 is connected with the cold side inlet of the second heat exchanger 20, and the cold side outlet of the second heat exchanger 20 is connected with the cold side inlet of the third heat exchanger 21; the cold side outlet of the third heat exchanger 21 is connected with the liquid inlet of the second tower stage of the desorption tower 11; the first liquid outlet at the bottom of the desorption tower 11 is connected with the cold side inlet of the reboiler 23, and the cold side outlet of the reboiler 23 is connected with the first liquid inlet at the bottom of the desorption tower 11 (the desorption tower 11 forms a thermal cycle with the reboiler 23 through the first liquid outlet and the first liquid inlet); the second liquid outlet at the bottom of the desorption tower 11 is connected with the inlet of the flash tank 24, and the gas outlet at the top of the desorption tower 11 is connected with the gas inlet of the carbon dioxide water scrubber 28; the gas outlet of the flash tank gas 24 is connected with the inlet of the vapor compressor 25, and the liquid outlet of the flash tank 24 is connected with the inlet of the lean liquid pump 26; the outlet of the vapor compressor 25 is connected with the hot side inlet of the second heat exchanger 20, and the hot side outlet of the second heat exchanger 20 is connected with the first gas inlet at the bottom of the desorption tower 11; the outlet of the lean liquid pump 26 is connected with the hot side inlet of the first heat exchanger 19, and the hot side outlet of the first heat exchanger 19 is connected with the inlet of the absorption liquid storage tank 27; the outlet of the absorption liquid storage tank 27 is connected with the inlet of the absorption liquid pump 41, the outlet of the absorption liquid pump 41 is connected with the inlet of the absorption liquid cooler 15, and the outlet of the absorption liquid cooler 15 is connected with the liquid inlet at the top of the absorption tower 10. The bottom gas inlet and the liquid outlet of the carbon dioxide water scrubber 28 are respectively connected with the top gas outlet and the top liquid inlet of the desorption tower 11, and the top gas outlet and the liquid inlet of the carbon dioxide water scrubber 28 are respectively connected with the inlet of the condenser 30 and the liquid outlet of the gas-liquid separator 31; the inlet and the gas outlet of the gas-liquid separator 31 are respectively connected with the outlet of the condenser 31 and the inlet of the gas compressor 32; the outlet of the gas compressor 32 is connected to the inlet of a gas cooler 33.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.
Claims (4)
1. The device for absorbing and capturing carbon dioxide by an amine method comprises an absorption tower, a desorption tower, an exhaust channel communicated with the desorption tower, an air inlet channel and an air outlet channel respectively communicated with the absorption tower, a reboiler for providing heat for the desorption tower, a lean solution channel respectively communicated with the absorption tower and the desorption tower, and a rich solution channel respectively communicated with the absorption tower and the desorption tower; the method is characterized in that: the heat recovery mechanism is used for recovering residual heat left in the desorption tower when carbon dioxide is released and transmitting the residual heat into the rich liquid channel;
the heat recovery mechanism comprises a first heat exchanger, and the lean liquid channel exchanges heat with the rich liquid channel through the first heat exchanger; the heat recovery mechanism further comprises a second heat exchanger and a flash tank arranged on the lean liquid channel; the flash tank has a vapor passage in communication with the desorber; the steam channel exchanges heat with the rich liquid channel through the second heat exchanger; a vapor compressor is further arranged on the vapor channel at the upstream of the second heat exchanger; the third heat exchanger is further included, and the rich liquid channel exchanges heat with the water outlet pipe of the reboiler through the third heat exchanger;
The hot rich liquid is desorbed and regenerated to form hot lean liquid, the hot lean liquid is discharged from the bottom outlet of the desorption tower, enters the flash tank through the inlet of the flash tank, and the generated flash steam and medium Wen Pinye are respectively discharged from the top outlet and the bottom outlet of the flash tank; the flash steam enters the steam compressor from the inlet of the steam compressor, is compressed to become high-temperature high-pressure compressed steam, and is discharged; the compressed steam enters the second heat exchanger from a hot side inlet of the second heat exchanger and becomes saturated steam after being cooled down; the saturated steam enters the desorption tower from a gas inlet at the bottom of the desorption tower to supply heat;
Further comprises: a rich liquid pump, a carbon dioxide water scrubber and a lean liquid pump; the liquid outlet of the absorption tower is connected with the inlet of the rich liquid pump, and the rich liquid pump is connected with the cold side inlet of the first heat exchanger; the first heat exchanger cold side outlet is connected with the second heat exchanger cold side inlet, and the second heat exchanger cold side outlet is connected with the third heat exchanger cold side inlet; the cold side outlet of the third heat exchanger is connected with the liquid inlet of the second tower stage of the desorption tower; the first liquid outlet at the bottom of the desorption tower is connected with the cold side inlet of the reboiler, the cold side outlet of the reboiler is connected with the first liquid inlet at the bottom of the desorption tower, and the desorption tower forms a thermal cycle with the reboiler through the first liquid outlet and the first liquid inlet; the second liquid outlet at the bottom of the desorption tower is connected with the inlet of the flash tank, and the gas outlet at the top of the desorption tower is connected with the gas inlet of the carbon dioxide water scrubber; the flash tank gas outlet is connected with the vapor compressor inlet, and the flash tank liquid outlet is connected with the lean liquid pump inlet; the outlet of the vapor compressor is connected with the hot side inlet of the second heat exchanger, and the hot side outlet of the second heat exchanger is connected with the first gas inlet at the bottom of the desorption tower;
the exhaust passage exchanges heat with the rich liquid passage through the fourth heat exchanger;
The system further comprises a fifth heat exchanger, wherein a gas compressor is arranged on the exhaust passage, and the exhaust passage at the downstream of the gas compressor exchanges heat with the rich liquid passage through the fifth heat exchanger.
2. The device for absorbing and capturing carbon dioxide by an amine method according to claim 1, wherein: the absorption tower also comprises a tower-stage cooler for cooling absorption liquid, wherein a liquid inlet and a liquid outlet of the tower-stage cooler are respectively communicated with the absorption tower.
3. The device for absorbing and capturing carbon dioxide by an amine method according to claim 1, wherein: the device comprises a gas inlet, a gas outlet, a gas inlet channel, a gas outlet, a gas inlet channel and a gas outlet channel.
4. The device for absorbing and capturing carbon dioxide by an amine method according to claim 1, wherein: the flue gas water scrubber for spraying water is characterized by further comprising a flue gas water scrubber for spraying water, wherein the bottom of the flue gas water scrubber is provided with a second flue gas inlet, the top of the flue gas water scrubber is provided with a second flue gas outlet communicated with an external space, and the second flue gas inlet is communicated with the exhaust channel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910257422.XA CN110013740B (en) | 2019-04-01 | 2019-04-01 | Device for absorbing and capturing carbon dioxide by amine method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910257422.XA CN110013740B (en) | 2019-04-01 | 2019-04-01 | Device for absorbing and capturing carbon dioxide by amine method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110013740A CN110013740A (en) | 2019-07-16 |
| CN110013740B true CN110013740B (en) | 2024-10-22 |
Family
ID=67190344
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910257422.XA Active CN110013740B (en) | 2019-04-01 | 2019-04-01 | Device for absorbing and capturing carbon dioxide by amine method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110013740B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111729483A (en) * | 2020-07-23 | 2020-10-02 | 中国华电科工集团有限公司 | A carbon dioxide capture system and method |
| CN113828120A (en) * | 2021-11-01 | 2021-12-24 | 中国船舶重工集团公司第七一一研究所 | Low-energy-consumption marine diesel engine flue gas CO2Trapping system |
| CN114788992A (en) * | 2022-03-09 | 2022-07-26 | 国家电投集团远达环保股份有限公司 | Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system |
| CN115523004B (en) * | 2022-10-18 | 2023-07-11 | 北京源碳环境股份有限公司 | Amine process CO 2 Combined power generation device and method for recovering heat energy of process medium in trapping device |
| CN115654760A (en) * | 2022-10-31 | 2023-01-31 | 北京百利时能源技术股份有限公司 | A multi-stage heat pump cascade recovery and analysis system for waste heat in a CO2 capture device |
| CN115738601A (en) * | 2022-12-01 | 2023-03-07 | 安徽普泛能源技术有限公司 | Gas removing and pressure increasing equipment and process |
| CN116212593B (en) * | 2023-04-18 | 2024-07-02 | 河北正元氢能科技有限公司 | Cryogenic carbon dioxide trapping device for urea production |
| CN119746586B (en) * | 2025-01-14 | 2025-11-07 | 中国华能集团清洁能源技术研究院有限公司 | CO capture for electrochemical mediated amine regeneration2Is a system of (2) |
| CN120771703B (en) * | 2025-09-10 | 2025-11-11 | 北京市弘洁蓝天科技股份有限公司 | A separation device and process for externally heated and recycled carbon dioxide |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20150015885A (en) * | 2013-08-02 | 2015-02-11 | 한국전력공사 | Apparatus and Method for Sour Gas Treating |
| 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 |
| CN109092020A (en) * | 2018-10-24 | 2018-12-28 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system suitable for phase transformation absorbent |
| CN210021644U (en) * | 2019-04-01 | 2020-02-07 | 中国能源建设集团广东省电力设计研究院有限公司 | Device for absorbing and capturing carbon dioxide by amine method |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202844827U (en) * | 2012-09-26 | 2013-04-03 | 中国恩菲工程技术有限公司 | Smoke gas desulfurization system |
| JP2016112482A (en) * | 2014-12-11 | 2016-06-23 | 三菱日立パワーシステムズ株式会社 | Carbon dioxide collection method and device |
-
2019
- 2019-04-01 CN CN201910257422.XA patent/CN110013740B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20150015885A (en) * | 2013-08-02 | 2015-02-11 | 한국전력공사 | Apparatus and Method for Sour Gas Treating |
| 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 |
| CN109092020A (en) * | 2018-10-24 | 2018-12-28 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system suitable for phase transformation absorbent |
| CN210021644U (en) * | 2019-04-01 | 2020-02-07 | 中国能源建设集团广东省电力设计研究院有限公司 | Device for absorbing and capturing carbon dioxide by amine method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110013740A (en) | 2019-07-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110013740B (en) | Device for absorbing and capturing carbon dioxide by amine method | |
| CN114768488B (en) | Coal-fired unit flue gas carbon dioxide entrapment system | |
| CN102671510B (en) | The recovery process of flue gas CO2 | |
| CN113877365A (en) | CO2Trapping system and process | |
| CN103096999A (en) | Jet engine with carbon capture | |
| CN212166984U (en) | CO2 capture system | |
| CN107859539A (en) | A kind of double Brayton cycle electricity generation systems of carbon dioxide of integrated carbon trapping | |
| CN115212708A (en) | Low-cost organic amine method flue gas carbon dioxide capture system and capture method thereof | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN106955569B (en) | A kind of hydrate continuously traps CO in cement kiln flue gas2Method | |
| CN219539893U (en) | Carbon dioxide trapping system and carbon dioxide treatment system | |
| CN103143248A (en) | System for absorbing and desorbing low-content CO2 in industrial exhaust gas | |
| CN210021644U (en) | Device for absorbing and capturing carbon dioxide by amine method | |
| CN111437710A (en) | A kind of alcohol-amine-water carbon dioxide capture liquid and carbon dioxide capture method | |
| CN110152453A (en) | Use the method and apparatus of sour gas in solvent absorption captured gas mixture | |
| CN116492814A (en) | A flue gas carbon dioxide capture process system | |
| CN117000005A (en) | A system and method for capturing carbon dioxide in flue gas | |
| KR20130010253A (en) | Method of resource reuse of stripping system for acid gas capture | |
| CN108854423A (en) | A kind of method for the flue gas purification system and fume treatment that the desulphurization and denitration of fume afterheat driving is coupled with carbon capture | |
| CN219815797U (en) | Ship CO capable of being flexibly arranged 2 Trapping system | |
| CN114632402A (en) | Flue gas carbon dioxide capture system and capture method | |
| CN120268190B (en) | A wet decarbonization technology regeneration gas heat recovery process system | |
| KR20260002532A (en) | Acid gas absorbing systemfor absorbing acid gas using the same | |
| CN112933895B (en) | Carbon dioxide trapping energy-saving separation system | |
| CN119034456B (en) | A carbon dioxide chemical absorption and capture multi-energy complementary regeneration heating system and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |