CN110152457B - Chemical absorption method carbon dioxide trapping system based on waste heat recycling - Google Patents
Chemical absorption method carbon dioxide trapping system based on waste heat recycling Download PDFInfo
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- CN110152457B CN110152457B CN201910409729.7A CN201910409729A CN110152457B CN 110152457 B CN110152457 B CN 110152457B CN 201910409729 A CN201910409729 A CN 201910409729A CN 110152457 B CN110152457 B CN 110152457B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 215
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 210
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 105
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 105
- 239000002918 waste heat Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 39
- 239000000126 substance Substances 0.000 title claims abstract description 35
- 238000004064 recycling Methods 0.000 title claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 428
- 238000003795 desorption Methods 0.000 claims abstract description 143
- 239000002250 absorbent Substances 0.000 claims abstract description 130
- 230000002745 absorbent Effects 0.000 claims abstract description 130
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 115
- 239000003546 flue gas Substances 0.000 claims abstract description 115
- 239000007921 spray Substances 0.000 claims abstract description 8
- 238000005406 washing Methods 0.000 claims description 162
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 69
- 239000006096 absorbing agent Substances 0.000 claims description 35
- 239000007789 gas Substances 0.000 claims description 29
- 238000000746 purification Methods 0.000 claims description 29
- 150000001412 amines Chemical class 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 17
- 238000010926 purge Methods 0.000 claims description 16
- 239000012629 purifying agent Substances 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 9
- 229920006395 saturated elastomer Polymers 0.000 claims description 9
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical group [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 4
- 230000002378 acidificating effect Effects 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000005201 scrubbing Methods 0.000 description 4
- 239000002516 radical scavenger Substances 0.000 description 3
- KXDHJXZQYSOELW-UHFFFAOYSA-M Carbamate Chemical compound NC([O-])=O KXDHJXZQYSOELW-UHFFFAOYSA-M 0.000 description 2
- 206010067484 Adverse reaction Diseases 0.000 description 1
- 230000006838 adverse reaction Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000011165 process development Methods 0.000 description 1
- 230000000630 rising effect Effects 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/02—Heat pumps of the compression type
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
- F25B41/30—Expansion means; Dispositions thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
- F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a chemical absorption method carbon dioxide capturing system based on waste heat recycling, which comprises an absorption tower, a rich liquid pump, a first lean-rich liquid heat exchanger, a rich liquid splitter, a second lean-rich liquid heat exchanger, a heat pump system, a desorption tower, a boiler, a lean liquid pump and a lean liquid cooler. The flue gas enters the absorption tower and moves from bottom to top, the absorbent enters the absorption tower and sprays downwards, and the absorbent contacts with the flue gas in a countercurrent way, so that the absorbent absorbs carbon dioxide in the flue gas to become rich liquid; the rich liquid enters a rich liquid pump and then enters a first lean rich liquid heat exchanger to absorb heat and raise temperature; the rich liquid after the first heat exchange enters a rich liquid splitter to split into two paths, the first path of rich liquid enters a heat pump system to absorb heat and raise temperature, and then the first path of rich liquid enters a desorption tower; the second path of rich liquid enters a second lean and rich liquid heat exchanger to absorb heat and raise temperature, and then the second path of rich liquid is subjected to a desorption tower; the first and second rich liquids are heated in a desorber to desorb and decompose into lean liquid and carbon dioxide.
Description
Technical Field
The invention relates to the field of waste heat recovery, in particular to a chemical absorption method carbon dioxide capturing system based on waste heat recovery.
Background
As the content of CO 2 in the atmosphere is continuously rising due to the massive combustion of fossil fuels, the greenhouse effect is becoming more and more serious due to the emission of massive CO 2, and the control of the emission of CO 2 has become a focus of attention of various countries.
The organic amine capture CO 2 technology is the most mature technology at present. The principle and flow of the organic amine for capturing CO 2 are as follows: CO 2 in the flue gas reacts with organic amine in an absorption tower to generate carbamate, and the carbamate is conveyed to a desorption tower to be heated, decomposed and reduced into organic amine and carbon dioxide, and the organic amine solution returns to the absorption tower to be absorbed again. The process of capturing CO 2 by the organic amine carbon capturing method is widely used because of the rapid absorption rate, high absorption efficiency, simple process and mature technology; however, the technology of capturing CO 2 by using organic amine has higher energy consumption, and how to recycle waste heat in lean solution and gas obtained by desorption of a desorption tower is a main way for reducing energy consumption, and is also a main foothold for energy-saving process development.
Disclosure of Invention
In view of the problems in the prior art, an object of the present invention is to provide a chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization, which can effectively utilize the heat of the gas discharged from the top of a desorption tower to heat a rich liquid, improve the utilization rate of waste heat, and reduce the heat required for desorption of the rich liquid.
In order to achieve the above object, the invention provides a chemical absorption method carbon dioxide capturing system based on waste heat recycling, which comprises an absorption tower, a rich liquid pump, a first lean-rich liquid heat exchanger, a rich liquid splitter, a second lean-rich liquid heat exchanger, a heat pump system, a desorption tower, a boiler, a lean liquid pump and a lean liquid cooler. The absorption tower comprises: the first inlet of the absorption tower is positioned at the lower part of the absorption tower and is used for allowing flue gas to enter, and the flue gas contains carbon dioxide; the second inlet of the absorption tower is positioned at the upper part of the absorption tower and is used for the absorbent to enter; the first outlet of the absorption tower is positioned at the bottom of the absorption tower and is used for flowing out the rich liquid; and the second outlet of the absorption tower is positioned at the top of the absorption tower. The rich liquid pump includes: the rich liquid pump inlet is communicated with the first outlet of the absorption tower; and an outlet of the rich liquid pump. The first lean-rich liquid heat exchanger includes: a first inlet of the first lean-rich liquid heat exchanger is communicated with an outlet of the rich liquid pump; a first lean-rich liquid heat exchanger second inlet; a first outlet of the first lean-rich liquid heat exchanger; and a second outlet of the first lean-rich liquid heat exchanger. The rich liquid splitter includes: the rich liquid diverter inlet is communicated with a first outlet of the first lean rich liquid heat exchanger; a rich liquid splitter first outlet; and a second outlet of the rich liquid splitter. The second lean-rich liquid heat exchanger includes: the first inlet of the second lean-rich liquid heat exchanger is communicated with the second outlet of the rich liquid splitter; a second inlet of the second lean-rich liquid heat exchanger; a second lean-rich liquid heat exchanger first outlet; and the second outlet of the second lean-rich liquid heat exchanger is communicated with the second inlet of the first lean-rich liquid heat exchanger. The heat pump system includes an evaporator, a compressor, a condenser, and a throttle valve. The evaporator comprises: an evaporator first inlet; an evaporator second inlet; an evaporator first outlet; and a second outlet of the evaporator. The compressor includes: a compressor inlet communicated with the second outlet of the evaporator; and a compressor outlet. The condenser includes: a first condenser inlet is communicated with a first rich liquor shunt outlet; a condenser second inlet communicated with the compressor outlet; a condenser first outlet; and a condenser second outlet. The throttle valve is arranged between the condenser and the evaporator, one end of the throttle valve is controlled to be communicated with the second outlet of the condenser, and the other end of the throttle valve is controlled to be communicated with the second inlet of the evaporator. The desorber includes: the first inlet of the desorption tower is positioned at the upper part of the desorption tower and is communicated with the first outlet of the condenser; the second inlet of the desorption tower is positioned at the upper part of the desorption tower and is lower than the first inlet of the desorption tower, and is communicated with the first outlet of the second lean-rich liquid heat exchanger; a third inlet of the desorption tower is positioned in the middle of the desorption tower and is lower than the second inlet of the desorption tower; a fourth inlet of the desorption tower is positioned at the lower part of the desorption tower and is lower than the third inlet of the desorption tower; the first outlet of the desorption tower is positioned at the top of the desorption tower and is communicated with the first inlet of the evaporator; the second outlet of the desorption tower is positioned at the bottom of the desorption tower; and a third outlet of the desorption tower is positioned at the lower part of the desorption tower. The boiler comprises: the first inlet of the boiler is communicated with the third outlet of the desorption tower; a second inlet of the boiler for inflow of external saturated steam; the first outlet of the boiler is communicated with the fourth inlet of the desorption tower; a second outlet of the boiler. The lean solution pump includes: the lean solution pump inlet is communicated with the second outlet of the first lean solution heat exchanger; lean liquid pump outlet. One side of the lean solution cooler is communicated with the lean solution pump outlet, and the other side of the lean solution cooler is communicated with the second inlet of the absorption tower.
The flue gas enters the absorption tower from the first inlet of the absorption tower and moves from bottom to top, the absorbent enters the absorption tower from the second inlet of the absorption tower and sprays downwards, the downwards sprayed absorbent contacts with the flue gas in a countercurrent way, so that the absorbent absorbs carbon dioxide in the flue gas to become rich liquid, the rich liquid is settled downwards, and the flue gas from which the carbon dioxide is removed continues to move upwards;
the rich liquid enters a rich liquid pump through a first outlet of the absorption tower and a rich liquid pump inlet, and then enters a first lean and rich liquid heat exchanger through a rich liquid pump outlet and a first inlet of the first lean and rich liquid heat exchanger to perform first heat exchange so as to absorb heat and raise temperature;
the rich liquid after the first heat exchange enters the rich liquid splitter through the first outlet of the first lean-rich liquid heat exchanger and the inlet of the rich liquid splitter to split into two paths,
The first path of rich liquid enters the condenser through the first outlet of the rich liquid splitter and the first inlet of the condenser to perform second heat exchange and absorb heat to raise temperature, and the first path of rich liquid after finishing the second heat exchange enters the desorber through the first outlet of the condenser and the first inlet of the desorber;
the second path of rich liquid enters the second lean and rich liquid heat exchanger through the second outlet of the rich liquid splitter and the first inlet of the second lean and rich liquid heat exchanger to perform third heat exchange and absorb heat to raise temperature, and the second path of rich liquid after the third heat exchange enters the desorber through the first outlet of the second lean and rich liquid heat exchanger and the second inlet of the desorber;
the first path of rich liquid and the second path of rich liquid are heated and desorbed in a desorption tower and decomposed into lean liquid and carbon dioxide, the lean liquid is settled downwards in the desorption tower, and the carbon dioxide moves upwards;
Part of liquid at the bottom of the desorption tower enters the boiler through a third outlet of the desorption tower and a first inlet of the boiler and performs fourth heat exchange with saturated steam flowing in through a second inlet of the boiler, and the part of liquid absorbs heat in the boiler to be heated up to be partially vaporized and enters the desorption tower through the first outlet of the boiler and the fourth inlet of the desorption tower, so that steam and heat are provided for desorption of rich liquid in the desorption tower; the saturated steam in the boiler releases heat and is cooled to become condensed water, and the condensed water is discharged through a second outlet of the boiler;
The upward carbon dioxide carries partial lean liquid, then enters the evaporator through a first outlet of the desorption tower and a first inlet of the evaporator to perform fifth heat exchange with working medium liquid in the evaporator, the working medium liquid absorbs heat and rises temperature to become working medium steam, the working medium steam enters the compressor through a second outlet of the evaporator and a compressor inlet, the compressor compresses the working medium steam, the compressed working medium steam rises temperature and rises pressure to become superheated steam, the superheated steam enters the condenser through the compressor outlet and a second inlet of the condenser and performs the second heat exchange with a first rich liquid flowing in through the first inlet of the condenser, the first rich liquid absorbs heat and rises temperature, the superheated steam releases heat and lowers temperature to become high-pressure working medium liquid, the high-pressure liquid flows into the throttle valve and is depressurized to become the working medium liquid in an initial state, and the working medium liquid enters the evaporator again through the second inlet of the evaporator under the action of the throttle valve, so that the working medium liquid completes a cycle using process;
the lean solution desorbed from the desorption tower enters the second lean-rich solution heat exchanger through the second outlet of the desorption tower and the second inlet of the second lean-rich solution heat exchanger, and performs the third heat exchange with the second path of rich solution entering through the first inlet of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled;
The lean solution after finishing the third heat exchange enters the first lean-rich solution heat exchanger through the second outlet of the second lean-rich solution heat exchanger and the second inlet of the first lean-rich solution heat exchanger, performs the first heat exchange with the rich solution entering through the first inlet of the first lean-rich solution heat exchanger, releases heat and lowers the temperature of the lean solution, the lean solution after finishing the first heat exchange enters the lean solution cooler through the second outlet of the first lean-rich solution heat exchanger and the lean solution pump to be cooled again, and then the cooled lean solution enters the absorption tower through the lean solution cooler and the second inlet of the absorption tower to be used as an absorbent for absorbing carbon dioxide.
In one embodiment, the absorber further comprises: the third inlet of the absorption tower is positioned in the middle of the absorption tower and below the second inlet of the absorption tower; the third outlet of the absorption tower is positioned in the middle of the absorption tower and above the third inlet of the absorption tower. The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises an inter-stage cooler, wherein one side of the inter-stage cooler is communicated with the third inlet of the absorption tower, and the other side of the inter-stage cooler is communicated with the third outlet of the absorption tower. The absorber in the absorption tower flows into the inter-stage cooler through a third outlet of the absorption tower to cool, the absorber cooled through the inter-stage cooler flows back into the absorption tower through a third inlet of the absorption tower and is sprayed downwards, the downwards sprayed absorber contacts with flue gas entering through a first inlet of the absorption tower in a countercurrent way, at least part of carbon dioxide in the flue gas is absorbed by the absorber to become rich liquid, and the rich liquid is settled downwards; the flue gas from which at least part of carbon dioxide is removed continues to move upwards and is in countercurrent contact with the absorbent sprayed down through the second inlet of the absorption tower again, and the flue gas is reacted for the second time by the absorbent sprayed down through the second inlet of the absorption tower to become rich liquid and flue gas from which carbon dioxide is removed, the generated rich liquid is settled downwards, the flue gas from which carbon dioxide is removed still continues to move upwards, and the flue gas from which carbon dioxide is removed, which moves upwards, carries part of the absorbent.
In one embodiment, the absorber further comprises: a fourth inlet of the absorption tower is positioned at the upper part of the absorption tower and at the upper part of the second inlet of the absorption tower; and a fourth outlet of the absorption tower is positioned at the upper part of the absorption tower and above the second inlet of the absorption tower, and is used for flowing out the pre-stored water washing water in the absorption tower. The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises a primary washing pump and a primary washing cooler. The primary washing pump includes: the primary washing pump inlet is communicated with the fourth outlet of the absorption tower; and a primary washing pump outlet. One side of the primary washing cooler is communicated with the outlet of the primary washing pump, and the other side is communicated with the fourth inlet of the absorption tower. After the primary washing pump is started, water washing water in the absorption tower flows into the primary washing pump through a fourth outlet of the absorption tower and a primary washing pump inlet, then flows into the primary washing cooler through a primary washing pump outlet for cooling, the cooled water washing water flows back to the upper part of the absorption tower again and sprays downwards, carbon dioxide is removed, flue gas carrying part of absorbent moves upwards in the absorption tower and is contacted with the cooled water washing water in a countercurrent mode, at least part of absorbent in the flue gas is dissolved in the water washing water, and the flue gas after primary washing continues to move upwards and is discharged through a second outlet of the absorption tower.
In one embodiment, the flue gas exiting through the second outlet of the absorber tower also carries a portion of the absorbent. The chemical absorption method carbon dioxide trapping system based on waste heat recycling also comprises a first gas-liquid separator, a washing tower, a secondary washing pump, a secondary washing cooler, a lean solution splitter and an absorbent storage. The first gas-liquid separator includes: the first gas-liquid separator inlet is communicated with the second outlet of the absorption tower; the first outlet of the first gas-liquid separator is positioned at the bottom of the first gas-liquid separator; the second outlet of the first gas-liquid separator is positioned at the top of the first gas-liquid separator. The washing tower is stored with water washing water, and the washing tower comprises: the first inlet of the washing tower is positioned in the middle of the washing tower and is communicated with the second outlet of the first gas-liquid separator; a second inlet of the washing tower is positioned at the upper part of the washing tower; the first outlet of the washing tower is positioned at the top of the washing tower; the second outlet of the washing tower is positioned at the lower part of the washing tower; and a third outlet of the washing tower is positioned at the bottom of the washing tower. The secondary washing pump includes: the inlet of the secondary washing pump is communicated with the second outlet of the washing tower; and a secondary washing pump outlet. One side of the secondary washing cooler is communicated with an outlet of the secondary washing pump, and the other side of the secondary washing cooler is communicated with a second inlet of the washing tower. The lean solution splitter includes: the lean solution diverter first inlet is communicated with the first gas-liquid separator first outlet; the second inlet of the lean solution splitter is communicated with the third outlet of the washing tower; and a lean liquid diverter outlet. The absorbent reservoir includes: an absorbent reservoir inlet communicating with the lean liquid diverter outlet; and an absorbent reservoir outlet communicated with one side of the lean solution cooler.
Wherein the flue gas which is discharged from the second outlet of the absorption tower and carries part of the absorbent enters the first gas-liquid separator through the inlet of the first gas-liquid separator, the first gas-liquid separator separates at least part of the absorbent from the flue gas,
The flue gas is discharged through a second outlet of the first gas-liquid separator, the discharged flue gas still contains at least part of absorbent, the flue gas containing at least part of absorbent enters the washing tower through a first inlet of the washing tower and moves upwards, water washing water in the washing tower enters a secondary washing pump through a second outlet of the washing tower and an inlet of a secondary washing pump, then flows into a secondary washing cooler through an outlet of the secondary washing pump for cooling, cooled water washing water enters the washing tower through a second inlet of the washing tower and is sprayed downwards, sprayed water washing water is in countercurrent contact with the flue gas carrying at least part of absorbent, the absorbent in the flue gas is dissolved by the water washing water, the flue gas with the absorbent removed is discharged through the first outlet of the washing tower, and the water washing water with the absorbent is dissolved flows into a lean liquid splitter through a third outlet of the washing tower and a second inlet of the lean liquid splitter;
The absorbent separated by the first gas-liquid separator flows into the lean liquid splitter through the first outlet of the first gas-liquid separator and the first inlet of the lean liquid splitter;
The lean solution splitter mixes the two paths of absorbent, the mixed absorbent enters the absorbent storage through the outlet of the lean solution splitter and the inlet of the absorbent storage, and then flows into the absorption tower through the outlet of the absorbent storage and the lean solution cooler to be recycled.
In one embodiment, the chemical absorption method carbon dioxide capturing system based on waste heat recycling further comprises a flash tank, a Roots blower and a steam cooler. The flash tank includes: the flash tank inlet is communicated with the second outlet of the desorption tower; a flash tank first outlet; and the second outlet of the flash tank is communicated with the second inlet of the second lean-rich liquid heat exchanger. Roots blower includes: the Roots blower inlet is communicated with the first outlet of the flash tank; roots blower outlet. One side of the steam cooler is communicated with the Roots blower outlet, and the other side is communicated with the third inlet of the desorption tower.
The lean solution flowing out from the second outlet of the desorption tower directly enters the flash tank through the inlet of the flash tank, the lean solution is flashed in the flash tank to flash part of steam, the flash steam enters the Roots blower through the first outlet of the flash tank and the inlet of the Roots blower, the steam is pressurized and heated in the Roots blower, and then enters the steam cooler for cooling through the outlet of the Roots blower, and the cooled steam enters the desorption tower through the third inlet of the desorption tower to provide auxiliary heat for desorption of the rich solution in the desorption tower; the lean solution after flash evaporation treatment enters the second lean-rich solution heat exchanger through the second outlet of the flash evaporation tank and the second inlet of the second lean-rich solution heat exchanger, and performs the third heat exchange with the second rich solution entering through the first inlet of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled.
In one embodiment, the chemical absorption method carbon dioxide capturing system based on waste heat recycling further comprises a purifying tower, a purifying pump and a purifying cooler. Purifying agent is stored in the purifying tower, and the purifying tower includes: the first inlet of the purifying tower is positioned at the lower part of the purifying tower and is used for entering external flue gas; a second inlet of the purifying tower is positioned at the upper part of the purifying tower; the first outlet of the purifying tower is positioned at the top of the purifying tower and is communicated with the first inlet of the absorption tower; the second outlet of the purifying tower is positioned at the lower part of the purifying tower and below the first inlet of the purifying tower. The purge pump includes: the inlet of the purifying pump is communicated with the second outlet of the purifying tower; purifying the pump outlet. One side of the purifying cooler is communicated with the outlet of the purifying pump, and the other side is communicated with the second inlet of the purifying tower.
The purifying tower, the purifying pump and the purifying cooler form an external flue gas purifying circulation loop, when the purifying pump is started, the purifying agent in the purifying tower is discharged through a second outlet of the purifying tower, pumped into the purifying cooler through the purifying pump to cool, then returned into the purifying tower through a second inlet of the purifying tower and sprayed downwards, the external flue gas enters the purifying tower through a first inlet of the purifying tower and moves upwards, the upwards-moved external flue gas is in countercurrent contact with the purifying agent sprayed downwards through the second inlet of the purifying tower, the purifying agent absorbs acidic impurity gas and smoke dust in the external flue gas, carbon dioxide in the external flue gas is not absorbed by the purifying agent, and the flue gas moves upwards and enters the absorbing tower through the first outlet of the purifying tower and the first inlet of the absorbing tower to be supplied to the absorbing tower.
In one embodiment, the scavenger is sodium bicarbonate solution.
In an embodiment, the carbon dioxide discharged from the first outlet of the desorber also carries a portion of the lean liquid. The chemical absorption method carbon dioxide trapping system based on waste heat recycling also comprises a desorption gas condenser and a second gas-liquid separator. Jie Xiqi the condenser comprises: jie Xiqi a condenser inlet communicated with a first outlet of the evaporator; and a desorber condenser outlet. The second gas-liquid separator includes: the inlet of the second gas-liquid separator is communicated with the outlet of the desorption gas condenser; the first outlet of the second gas-liquid separator is positioned at the top of the second gas-liquid separator; and a second outlet of the second gas-liquid separator is positioned at the bottom of the second gas-liquid separator.
The carbon dioxide with partial lean liquid enters the condenser through the first outlet of the evaporator and the inlet of the desorption gas condenser to be cooled, the cooled carbon dioxide with partial lean liquid enters the second gas-liquid separator through the inlet of the second gas-liquid separator, the carbon dioxide with partial lean liquid is separated into carbon dioxide product gas and lean liquid through the gas-liquid separation of the second gas-liquid separator, and the carbon dioxide product gas is discharged through the first outlet of the second gas-liquid separator to be subjected to the next operation;
The separated lean liquid is discharged through a second outlet of the second gas-liquid separator and then refluxed to the absorbent reservoir.
In one embodiment, the absorbent is an organic amine solution.
The beneficial effects of the invention are as follows: in the chemical absorption method carbon dioxide capturing system based on waste heat recycling, the heat pump system is arranged to effectively transfer the heat of the gas discharged from the top of the desorption tower to the rich liquid, so that the rich liquid absorbs heat and heats up, the heat required by desorption of the rich liquid in the desorption tower is reduced, the energy consumption is reduced, and the utilization rate of waste heat is improved.
Drawings
Fig. 1 is a schematic diagram of a chemical absorption carbon dioxide capture system based on waste heat recovery and utilization in accordance with the present invention.
Wherein reference numerals are as follows:
first outlet of 11 absorption tower 18B1 boiler
First inlet 18B2 of 11A1 absorption tower and second outlet of boiler
Lean solution pump at second inlet 19 of 11A2 absorption tower
11A3 absorber third inlet 19A lean solution pump inlet
11A4 absorber fourth inlet 19B lean solution pump inlet
Lean solution cooler at first outlet 20 of 11B1 absorption tower
11B2 absorber second outlet 21 inter-stage cooler
Primary washing pump for third outlet 22 of 11B3 absorption tower
11B4 absorber fourth outlet 22A primary washing pump inlet
12 Rich liquid pump 22B primary washing pump outlet
12A rich liquor pump inlet 23 primary washing cooler
12B rich liquid pump outlet 24 first gas-liquid separator
13 First lean-rich liquid heat exchanger 24A first gas-liquid separator inlet
13A1 first lean-rich liquid heat exchanger first 24B1 first gas-liquid separator first outlet
Inlet port
13A2 first lean-rich liquid heat exchanger second 24B2 first gas-liquid separator second outlet
Inlet port
13B1 first lean-rich liquid heat exchanger first 25 washing tower
Outlet 25A1 first inlet of the scrubber
13B2 first lean-rich liquid heat exchanger second inlet of second 25A2 washing tower
Outlet 25B1 first outlet of scrubber
Second outlet of 14 rich liquid splitter 25B2 washing tower
14A rich liquor splitter inlet 25B3 washing tower third outlet
Secondary washing pump for first outlet 26 of 14B1 rich liquor shunt
Second outlet 26A secondary wash pump inlet of 14B2 rich liquor splitter
15 Second lean-rich liquid heat exchanger 26B secondary washing pump outlet
15A1 second lean-rich liquid heat exchanger first 27 secondary washing cooler
Inlet 28 lean stream splitter
15A2 second lean-rich heat exchanger second 28A1 lean-rich flow divider first inlet
Inlet 28A2 lean stream splitter second inlet
15B1 second lean-rich liquid heat exchanger first 28B lean liquid diverter outlet
Outlet 29 absorbent reservoir
15B2 second lean rich liquid heat exchanger second 29A absorbent reservoir inlet
Outlet 29B absorbent reservoir outlet
16 Heat pump system 30 flash tank
161 Evaporator 30A flash tank inlet
161A1 evaporator first inlet 30B1 flash tank first outlet
161A2 evaporator second inlet 30B2 flash tank second outlet
161B1 evaporator first outlet 31 Roots blower
161B2 evaporator second outlet 31A Roots blower inlet
162 Compressor 31B Roots blower outlet
162A compressor inlet 32 vapor cooler
162B compressor outlet 33 purifying tower
163 Condenser 33A1 purifying column first inlet
163A1 condenser first inlet 33A2 purge column second inlet
163A2 condenser second inlet 33B1 purification column first outlet
163B1 condenser first outlet 33B2 purifying column second outlet
163B2 condenser second outlet 34 purge pump
164 Throttle valve 34A purge pump inlet
17 Desorber 34B purge pump outlet
17A1 desorber first inlet 35 purifying cooler
17A2 desorber second inlet 36 desorber gas condenser
17A3 desorber third inlet 36A Jie Xiqi condenser inlet
17A4 desorber fourth inlet 36B desorber condenser outlet
17B1 desorber first outlet 37 second gas-liquid separator
17B2 desorber second outlet 37A second gas-liquid separator inlet
17B3 desorber third outlet 37B1 second gas-liquid separator first outlet
18 Boiler mouth
Second outlet of second gas-liquid separator of first inlet 37B2 of 18A1 boiler
Second inlet of 18A2 boiler
Detailed Description
Referring to fig. 1, the chemical absorption method carbon dioxide capturing system based on waste heat recovery of the present invention includes an absorption tower 11, a rich liquid pump 12, a first lean-rich liquid heat exchanger 13, a rich liquid splitter 14, a second lean-rich liquid heat exchanger 15, a heat pump system 16, a desorption tower 17, a boiler 18, a lean liquid pump 19, and a lean liquid cooler 20.
The absorption tower 11 includes: the first inlet 11A1 of the absorption tower is positioned at the lower part of the absorption tower 11 and is used for allowing flue gas to enter, wherein the flue gas contains carbon dioxide; an absorber second inlet 11A2 located at the upper part of the absorber 11 for the entry of the absorbent; the first outlet 11B1 of the absorption tower is positioned at the bottom of the absorption tower 11 and is used for flowing out the rich liquid; the absorber second outlet 11B2 is located at the top of the absorber 11.
The rich liquid pump 12 includes: a rich liquid pump inlet 12A communicated with the first outlet 11B1 of the absorption tower; rich liquid pump outlet 12B.
The first lean-rich liquid heat exchanger 13 includes: the first inlet 13A1 of the first lean-rich liquid heat exchanger is communicated with the rich liquid pump outlet 12B; a first lean-rich liquid heat exchanger second inlet 13A2; a first lean-rich liquid heat exchanger first outlet 13B1; the first lean-rich liquid heat exchanger second outlet 13B2.
The rich liquid separator 14 includes: a rich liquid splitter inlet 14A communicated with a first lean rich liquid heat exchanger first outlet 13B1; a rich liquid splitter first outlet 14B1; the rich liquid splitter second outlet 14B2.
The second lean rich liquid heat exchanger 15 includes: the first inlet 15A1 of the second lean-rich liquid heat exchanger is communicated with the second outlet 14B2 of the rich liquid splitter; a second lean rich liquid heat exchanger second inlet 15A2; a second lean-rich liquid heat exchanger first outlet 15B1; the second outlet 15B2 of the second lean-rich liquid heat exchanger is communicated with the second inlet 13A2 of the first lean-rich liquid heat exchanger.
The heat pump system 16 includes an evaporator 161, a compressor 162, a condenser 163, and a throttle valve 164.
The evaporator 161 includes: an evaporator first inlet 161A1; an evaporator second inlet 161A2; an evaporator first outlet 161B1; and an evaporator second outlet 161B2.
The compressor 162 includes: a compressor inlet 162A communicating with the evaporator second outlet 161B2; compressor outlet 162B.
The condenser 163 includes: a condenser first inlet 163A1 communicating with the rich liquid splitter first outlet 14B1; a condenser second inlet 163A2 in communication with the compressor outlet 162B; a condenser first outlet 163B1; and a condenser second outlet 163B2.
A throttle valve 164 is provided between the condenser 163 and the evaporator 161, with one end being in controlled communication with the condenser second outlet 163B2 and the other end being in controlled communication with the evaporator second inlet 161A2.
The desorber 17 includes: a first inlet 17A1 of the desorption tower is positioned at the upper part of the desorption tower 17 and is communicated with a first outlet 163B1 of the condenser; a desorber second inlet 17A2 located at an upper portion of the desorber 17 and lower than the desorber first inlet 17A1 (preferably, located at a middle upper portion of the desorber 17) and communicating with the second lean-rich liquid heat exchanger first outlet 15B1; a desorber third inlet 17A3 located in the middle of the desorber 17 and lower than the desorber second inlet 17A2 (preferably, located in the middle lower part of the desorber 17); a fourth inlet 17A4 of the desorber, which is located at a lower portion of the desorber 17 and is lower than the third inlet 17A3 of the desorber; a first outlet 17B1 of the desorption tower is positioned at the top of the desorption tower 17 and is communicated with a first inlet 161A1 of the evaporator; a second outlet 17B2 of the desorption tower is positioned at the bottom of the desorption tower 17; the third outlet 17B3 of the desorption column is located at the lower part of the desorption column 17.
The boiler 18 includes: a boiler first inlet 18A1 is communicated with a third outlet 17B3 of the desorption tower; a boiler second inlet 18A2 into which external saturated steam flows; a boiler first outlet 18B1 is communicated with a fourth inlet 17A4 of the desorption tower; a boiler second outlet 18B2.
The lean liquid pump 19 includes: a lean solution pump inlet 19A is communicated with a second outlet 13B2 of the first lean solution heat exchanger; lean liquid pump outlet 19B.
Lean solution cooler 20 is connected to lean solution pump outlet 19B on one side and to absorber second inlet 11A2 on the other side.
The flue gas enters the absorption tower 11 through the first inlet 11A1 of the absorption tower and moves from bottom to top, the absorbent enters the absorption tower 11 through the second inlet 11A2 of the absorption tower and sprays downwards, and the absorbent sprayed downwards contacts with the flue gas in a countercurrent way, so that the absorbent absorbs carbon dioxide in the flue gas to become rich liquid, the rich liquid is settled downwards, and the flue gas from which the carbon dioxide is removed continues to move upwards. In one embodiment, the absorbent is an organic amine solution. Of course, not limited thereto, and other suitable absorbents may be selected by those skilled in the art.
The rich liquid enters the rich liquid pump 12 through the absorption tower first outlet 11B1 and the rich liquid pump inlet 12A, and then enters the first lean and rich liquid heat exchanger 13 through the rich liquid pump outlet 12B and the first lean and rich liquid heat exchanger first inlet 13A1 to perform first heat exchange so as to absorb heat and raise temperature.
The rich liquid having completed the first heat exchange enters the rich liquid splitter 14 via the first lean rich liquid heat exchanger first outlet 13B1, the rich liquid splitter inlet 14A to split into two paths.
The first rich liquid enters the condenser 163 through the first outlet 14B1 of the rich liquid splitter and the first inlet 163A1 of the condenser to perform the second heat exchange and absorb heat to raise temperature, and the first rich liquid after the second heat exchange enters the desorber 17 through the first outlet 163B1 of the condenser and the first inlet 17A1 of the desorber.
The second rich liquid enters the second lean-rich liquid heat exchanger 15 through the second outlet 14B2 of the rich liquid splitter and the first inlet 15A1 of the second lean-rich liquid heat exchanger to perform third heat exchange and absorb heat to raise temperature, and the second rich liquid after the third heat exchange enters the desorber 17 through the first outlet 15B1 of the second lean-rich liquid heat exchanger and the second inlet 17A2 of the desorber.
The first and second rich liquids are heated in the desorption tower 17 to be desorbed and decomposed into lean liquid and carbon dioxide, the lean liquid is settled down in the desorption tower 17, and the carbon dioxide moves upward.
A part of liquid (which may be a thoroughly desorbed lean liquid or a incompletely desorbed semi-lean liquid) at the bottom of the desorption tower 17 enters the boiler 18 through a third outlet 17B3 of the desorption tower and a first inlet 18A1 of the boiler and undergoes fourth heat exchange with saturated steam flowing in through a second inlet 18A2 of the boiler, absorbs heat in the boiler 18, heats up to be partially vaporized and enters the desorption tower 17 through the first outlet 18B1 of the boiler and the fourth inlet 17A4 of the desorption tower, and provides steam and heat for desorption of the rich liquid in the desorption tower 17; the saturated steam in the boiler 18 is cooled down by heat release to become condensed water, which is discharged through the boiler second outlet 18B 2. In the fourth heat exchange in the boiler 18, the semi-lean liquid is decomposed into steam, lean liquid, and carbon dioxide, and the three are returned to the desorption tower 17 together with a large amount of heat, and the carbon dioxide and steam with heat move upward in the desorption tower 17 to supply heat for the desorption of the two-way rich liquid.
The carbon dioxide moving upwards carries part of lean liquid (in the form of amine vapor), then enters the evaporator 161 through the first outlet 17B1 of the desorption tower and the first inlet 161A1 of the evaporator to perform fifth heat exchange with working medium liquid in the evaporator 161, the working medium liquid absorbs heat and rises to become working medium vapor, the working medium vapor enters the compressor 162 through the second outlet 161B2 of the evaporator and the inlet 162A of the compressor, the compressor 162 compresses the working medium vapor, the working medium vapor after compression rises to rise to become superheated vapor, the superheated vapor enters the condenser 163 through the outlet 162B of the compressor and the second inlet 163A2 of the condenser, the superheated vapor performs the second heat exchange with the first rich liquid flowing in through the first inlet 163A1 of the condenser, the first rich liquid absorbs heat and rises to become high-pressure working medium liquid, the high-pressure working medium liquid flows into the throttle valve 164 and is reduced to become the working medium liquid in an initial state, and the working medium liquid enters the evaporator again through the second inlet 161A2 of the evaporator under the action of the throttle valve 164, so that the working medium liquid completes a cycle using process.
The lean solution desorbed from the desorption tower 17 enters the second lean-rich solution heat exchanger 15 through the second outlet 17B2 of the desorption tower and the second inlet 15A2 of the second lean-rich solution heat exchanger, and undergoes the third heat exchange with the second rich solution entering through the first inlet 15A1 of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled.
The lean solution after the third heat exchange enters the first lean-rich solution heat exchanger 13 through the second outlet 15B2 of the second lean-rich solution heat exchanger and the second inlet 13A2 of the first lean-rich solution heat exchanger, performs the first heat exchange with the rich solution entering through the first inlet 13A1 of the first lean-rich solution heat exchanger, releases heat again to cool, and enters the lean solution cooler 20 through the second outlet 13B2 of the first lean-rich solution heat exchanger and the lean solution pump 19 to be cooled again, and then the cooled lean solution enters the absorber 11 through the lean solution cooler 20 and the second inlet 11A2 of the absorber to be used as an absorbent for absorbing carbon dioxide.
In the chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization according to the present invention, the rich liquid (cold rich liquid) discharged through the first outlet 11B1 of the absorption tower undergoes the first heat exchange under the action of the first lean-rich liquid heat exchanger 13 to absorb heat and raise temperature, and then is split into two paths through the rich liquid splitter 14, and the second path rich liquid undergoes the third heat exchange with the lean liquid (hot lean liquid) flowing out of the desorption tower 17 through the second lean-rich liquid heat exchanger 15, and then flows into the desorption tower 17 to be desorbed, thereby effectively utilizing the waste heat of the hot lean liquid; the heat carried by the carbon dioxide discharged from the top of the desorber 17 is indirectly absorbed by the first rich liquid through the heat transferred by the working medium in the heat pump system 16 (the gas discharged from the top of the desorber 17 and the working medium in the evaporator 16 perform fifth heat exchange, and the working medium absorbs heat and heats up), so that the waste heat of the gas at the top of the desorber 17 is effectively utilized to heat the first rich liquid; the two ways of rich liquid not only absorb the waste heat of the hot lean liquid flowing out from the bottom of the desorption tower 17, but also utilize the waste heat of the gas flowing out from the top of the desorption tower 17, and the rich liquid is divided into two ways compared with one way, so that the rich liquid absorbs more waste heat to reach higher temperature, the heat required by the rich liquid in desorption of the desorption tower 17 is reduced to a great extent, and the energy consumption of steam generated by the boiler 18 is further reduced.
The absorption tower 11 further includes: an absorber third inlet 11A3 located in the middle of the absorber 11 and below the absorber second inlet 11 A2; the third outlet 11B3 of the absorption column is located in the middle of the absorption column 11 and above the third inlet 11A3 of the absorption column.
The chemical absorption process carbon dioxide capture system based on waste heat recovery also includes an inter-stage cooler 21. The inter-stage cooler 21 is connected to the third inlet 11A3 of the absorber, and is connected to the third outlet 11B3 of the absorber.
Wherein the absorbent in the absorption tower 11 (absorbent sprayed down through the absorption tower second inlet 11A2 and stored in the absorption tower 11) flows into the inter-stage cooler 21 through the absorption tower third outlet 11B3 to be cooled, the absorbent cooled down through the inter-stage cooler 21 flows back into the absorption tower 11 through the absorption tower third inlet 11A3 and sprayed down, the sprayed-down absorbent contacts with the flue gas entering through the absorption tower first inlet 11A1 in a countercurrent manner, at least part of carbon dioxide in the flue gas is absorbed by the absorbent to become rich liquid, and the rich liquid is settled down; at least part of the carbon dioxide-removed flue gas continues to move upwards and is in countercurrent contact with the absorbent sprayed down through the second inlet 11A2 of the absorption tower again, and the absorbent sprayed down through the second inlet 11A2 of the absorption tower undergoes a second reaction to become rich liquid and carbon dioxide-removed flue gas, the generated rich liquid is settled downwards, the carbon dioxide-removed flue gas still continues to move upwards, and part of the absorbent is carried by the carbon dioxide-removed flue gas moving upwards.
It should be noted that, the absorption of carbon dioxide needs to be performed at a lower temperature, so as to ensure that the absorption amount of carbon dioxide in the absorption tower 11 reaches the maximum, and the arrangement of the inter-stage cooler 21 further reduces the temperature of the absorbent in the absorption tower 11, and the cooled absorbent flows back into the absorption tower 11 again to react with the flue gas, so that the absorption amount and absorption rate of carbon dioxide in the flue gas are improved, thereby reducing the use of the absorbent and saving the cost; the flue gas entering through the first inlet 11A1 of the absorption tower is absorbed by the absorbent sprayed down through the third inlet 11A3 of the absorption tower and the third inlet 11A2 of the absorption tower in sequence in the upward movement process, so that the carbon dioxide in the flue gas is fully absorbed, and the absorption rate of the carbon dioxide is improved.
In one embodiment, the inter-stage cooler 21 is a water cooler.
The upper chamber of the absorption tower 11 is pre-stored with washing water. The absorption tower 11 further includes: an absorber fourth inlet 11A4 located at an upper portion of the absorber 11 and above the absorber second inlet 11 A2; the fourth outlet 11B4 of the absorption tower is located at the upper part of the absorption tower 11 and above the second inlet 11A2 of the absorption tower, and is used for flowing out the water pre-stored in the absorption tower 11.
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises a primary washing pump 22 and a primary washing cooler 23.
The primary washing pump 22 includes: a primary washing pump inlet 22A connected to the fourth outlet 11B4 of the absorption column; a primary wash pump outlet 22B.
The primary scrubber cooler 23 is connected to the primary scrubber pump outlet 22B on one side and to the fourth inlet 11A4 of the absorber on the other side.
The absorption tower 11, the primary washing pump 22 and the primary washing cooler 23 form a primary washing loop, when the primary washing pump 22 is turned on, water washing water in the absorption tower 11 flows into the primary washing pump 22 through the fourth outlet 11B4 of the absorption tower and the inlet 22A of the primary washing pump, then flows into the primary washing cooler 23 through the outlet 22B of the primary washing pump for cooling, the cooled water washing water flows back to the upper part of the absorption tower 11 again and sprays down, the flue gas with carbon dioxide removed also carries part of absorbent when moving upwards in the absorption tower 11, the flue gas with carbon dioxide removed and part of absorbent moves upwards in the absorption tower 11 and contacts with the cooled water washing water in a countercurrent mode, at least part of absorbent in the flue gas is dissolved in the water washing water, and the flue gas after primary washing continues to move upwards and then is discharged through the second outlet 11B2 of the absorption tower.
At least the absorbent carried by the carbon dioxide-removed flue gas is washed in the primary washing process, the absorbent dissolved by the water washing is prevented from being carried out of the absorption tower 11 by the carbon dioxide-removed flue gas, and the loss of the absorbent is reduced.
In one embodiment, the absorption tower 11 further comprises a screen for an absorption tower, which is disposed at the top of the absorption tower 11, and is used for filtering amine vapor (absorbent) mixed in the flue gas for removing carbon dioxide, thereby further reducing the loss of the absorbent.
It should be noted that the flue gas that is subjected to the primary washing and then discharged through the second outlet 11B2 of the absorption tower still carries part of the absorbent.
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises a first gas-liquid separator 24 and a washing tower 25.
The first gas-liquid separator 24 includes: a first gas-liquid separator inlet 24A communicated with the second outlet 11B2 of the absorption tower; a first gas-liquid separator first outlet 24B1 located at the bottom of the first gas-liquid separator 24; the first gas-liquid separator second outlet 24B2 is located at the top of the first gas-liquid separator 24. In one embodiment, the first gas-liquid separator 24 further includes a first gas-liquid separator screen disposed on top of the first gas-liquid separator 24 for filtering condensed lean amine liquid (absorbent) mixed in the flue gas for removing carbon dioxide, thereby further reducing the loss of absorbent.
The washing tower 25 stores washing water, and the washing tower 25 includes: a first inlet 25A1 of the washing tower, which is positioned in the middle of the washing tower 25 and is communicated with a second outlet 24B2 of the first gas-liquid separator; a scrubber second inlet 25A2 located at an upper portion of the scrubber first inlet 25 A1; a scrubber first outlet 25B1 located at the top of the scrubber 25; a washing tower second outlet 25B2 located at a lower portion of the washing tower 25; the third outlet 25B3 of the scrubber is located at the bottom of the scrubber 25.
In an embodiment, the scrubbing tower 25 may further be provided with a screen for scrubbing tower, which is disposed at the top of the scrubbing tower 25, and is used for filtering condensed dilute amine solution (droplets) mixed in the flue gas for removing carbon dioxide, so as to further reduce the loss of absorbent.
The secondary washing pump 26 includes: a secondary washing pump inlet 26A communicated with a washing tower second outlet 25B2; and a secondary wash pump outlet 26B.
The secondary scrubber cooler 27 is connected to the secondary scrubber pump outlet 26B on one side and to the scrubber second inlet 25A2 on the other side.
Lean solution splitter 28 includes: lean liquid diverter first inlet 28A1 communicates with first gas-liquid separator first outlet 24B1; lean solution diverter second inlet 28A2, communicating scrubber third outlet 25B3; lean stream splitter outlet 28B.
The absorbent reservoir 29 includes: an absorber reservoir inlet 29A in communication with the lean splitter outlet 28B; the absorbent reservoir outlet 29B communicates with one side of the lean solution cooler 20.
Wherein the flue gas carrying part of the absorbent discharged from the second outlet 11B2 of the absorption tower enters the first gas-liquid separator 24 via the first gas-liquid separator inlet 24A, and the first gas-liquid separator 24 separates at least part of the absorbent from the flue gas.
The flue gas is discharged through the first gas-liquid separator second outlet 24B2, the discharged flue gas still contains at least part of the absorbent, the flue gas containing at least part of the absorbent enters the scrubber 25 through the scrubber first inlet 25A1 and moves upward, the water wash water in the scrubber 25 enters the secondary scrubber 26 through the scrubber second outlet 25B2 and the secondary scrubber pump inlet 26A, then flows into the secondary scrubber cooler 27 through the secondary scrubber pump outlet 26B to be cooled, the cooled water wash water enters the scrubber 25 through the scrubber second inlet 25A2 and sprays downward, the sprayed water wash water is in countercurrent contact with the flue gas carrying at least part of the absorbent, the absorbent in the flue gas is dissolved by the water wash water, the flue gas from which the absorbent is removed is discharged through the scrubber first outlet 25B1, and the water wash water from which the absorbent is dissolved flows into the lean liquid splitter 28 through the scrubber third outlet 25B3 and the lean liquid splitter second inlet 28 A2.
The absorbent separated via the first gas-liquid separator 24 flows into the lean liquid separator 28 via the first gas-liquid separator first outlet 24B1, the lean liquid separator first inlet 28 A1.
The lean solution splitter 28 mixes the above-described two paths of absorbent (the absorbent flowing in through the lean solution splitter first inlet 28A1 and the absorbent flowing in through the lean solution splitter second inlet 28 A2), and the mixed absorbent enters the absorbent reservoir 29 through the lean solution splitter outlet 28B and the absorbent reservoir 29 inlet, and then flows into the absorption tower 11 through the absorbent reservoir outlet 29B and the lean solution cooler 20 to be recycled.
In the secondary scrubbing process described above, the first gas-liquid separator 24 separates at least a portion of the absorbent in the flue gas before entering the lean liquid splitter 28; the flue gas subjected to gas-liquid separation enters the washing tower 25 again for secondary washing, the flue gas is washed by the washing tower 25, the absorbent carried by the flue gas is dissolved in the washing tower 25, then enters the lean liquid splitter 28, the absorbent separated by the first gas-liquid separator 24 and the absorbent washed by the washing tower 25 respectively flow into the lean liquid splitter 28 and are mixed, and the mixed absorbent returns to the absorption tower 11 again for recycling, so that the loss of the absorbent is greatly reduced, and the cost is saved; furthermore, the provision of the first gas-liquid separator wire mesh of the first gas-liquid separator 24 and the scrubber wire mesh of the scrubber 25 further reduces the loss of absorbent.
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises a flash tank 30, a Roots blower 31 and a steam cooler 32.
The flash tank 30 includes: a flash tank inlet 30A communicated with a second outlet 17B2 of the desorption tower; flash tank first outlet 30B1; the flash tank second outlet 30B2 communicates with the second lean-rich heat exchanger second inlet 15A2.
The Roots blower 31 includes: roots blower inlet 31A, communicating flash tank first outlet 30B1; roots blower outlet 31B.
The vapor cooler 32 is connected to the Roots blower outlet 31B on one side and to the third inlet 17A3 of the desorber on the other side.
The lean liquid flowing out through the second outlet 17B2 of the desorption tower directly enters the flash tank 30 through the flash tank inlet 30A, the lean liquid is flashed in the flash tank 30 to flash out part of steam (most of the steam is water vapor and the small part of the steam is amine vapor), the flash-out steam enters the roots blower 31 through the first outlet 30B1 of the flash tank and the roots blower inlet 31A, the steam is pressurized and heated in the roots blower 31, then enters the steam cooler 32 through the roots blower outlet 31B for cooling, and the cooled steam enters the desorption tower 17 through the third inlet 17A3 of the desorption tower to provide auxiliary heat for desorption of the rich liquid in the desorption tower 17; the lean liquid after the flash evaporation treatment enters the second lean-rich liquid heat exchanger 15 through the second outlet 30B2 of the flash evaporation tank and the second inlet 15A2 of the second lean-rich liquid heat exchanger, and performs the third heat exchange with the second rich liquid entering through the first inlet 15A1 of the second lean-rich liquid heat exchanger, so that the lean liquid releases heat and is cooled.
The lean solution is flashed to release a large amount of steam through the flash tank 30, the temperature and pressure of the steam are increased (for example, the steam is pressurized to 110-120 ℃ from 70-90 ℃) after the steam is pressurized by the Roots blower 31, the quality of the steam is greatly improved and is higher than the temperature of the lean solution in the desorption tower 17, and it is noted that if the steam temperature is too high (for example, more than 130 ℃), if the steam is directly introduced into the desorption tower 17, adverse reactions such as thermal degradation and the like occur to the desorbed lean solution, and the temperature of the hot steam can be reduced (reduced to below 130 ℃) by the steam cooler 32, so that the optimal desorption heat is provided for desorbing the rich solution by the desorption tower 17, meanwhile, the steam demand from the boiler 18 is reduced, and the energy consumption of the steam generated by the boiler 18 is reduced.
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises a purifying tower 33, a purifying pump 34 and a purifying cooler 35.
The purifying tower 33 stores a purifying agent, and the purifying tower 33 includes: a first inlet 33A1 of the purifying tower is positioned at the lower part of the purifying tower 33 for the external flue gas to enter; a purification tower second inlet 33A2 located at an upper portion of the purification tower 33; a purification tower first outlet 33B1 located at the top of the purification tower 33 and communicating with the absorption tower first inlet 11A1; the purification column second outlet 33B2 is located in the lower portion of the purification column 33 and below the purification column first inlet 33 A1.
In one embodiment, the purifying tower 33 further comprises a screen for the purifying tower for removing water vapor and mist from the flue gas.
The purge pump 34 includes: a purge pump inlet 34A communicating with the purge column second outlet 33B2; purge pump outlet 34B.
The purge cooler 35 has one side connected to the purge pump outlet 34B and the other side connected to the purge tower second inlet 33A2.
Wherein, the purifying tower 33, the purifying pump 34 and the purifying cooler 35 form an external flue gas purifying circulation loop, when the purifying pump 34 is started, the purifying agent in the purifying tower 33 is discharged through the purifying tower second outlet 33B2, pumped into the purifying cooler 35 through the purifying pump 34 for cooling, then returned into the purifying tower 33 through the purifying tower second inlet 33A2 and sprayed downwards, the external flue gas enters the purifying tower 33 through the purifying tower first inlet 33A1 and moves upwards, the upward moving external flue gas is in countercurrent contact with the purifying agent sprayed downwards through the purifying tower second inlet 33A2, the purifying agent absorbs acidic impurity gas and smoke dust in the external flue gas, carbon dioxide in the external flue gas is not absorbed by the purifying agent, and the flue gas moves upwards after being purified and enters the absorbing tower 11 through the purifying tower first outlet 33B1 and the absorbing tower first inlet 11A1 so as to be supplied to the absorbing tower 11.
In one embodiment, the first scrubber inlet 33A1 of the scrubber 33 may be in communication with a power plant flue gas duct. The scavenger may be sodium bicarbonate solution. Of course, not limited thereto, and any suitable scavenger may be selected by those skilled in the art.
The arrangement of the purifying tower 33 effectively purifies the flue gas entering the absorbing tower 11, prevents the absorbent in the absorbing tower 11 from absorbing impurity gas, and further improves the purity of the product gas.
The carbon dioxide discharged from the first outlet 17B1 of the desorber also carries a part of the lean liquid.
In an embodiment, the desorber 17 further comprises a screen for the desorber for filtering the amine vapor (lean liquid vapor) carried by the carbon dioxide, reducing the loss of a part of the lean liquid.
The chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization also comprises a desorption gas condenser 36 and a second gas-liquid separator 37.
Jie Xiqi the condenser 36 includes: jie Xiqi condenser inlet 36A, communicating with evaporator first outlet 161B1; desorber condenser outlet 36B.
The second gas-liquid separator 37 includes: a second gas-liquid separator inlet 37A in communication with the desorb gas condenser outlet 36B; a second gas-liquid separator first outlet 37B1 located at the top of the second gas-liquid separator 37; the second gas-liquid separator second outlet 37B2 is located at the bottom of the second gas-liquid separator 37.
In one embodiment, the second gas-liquid separator 37 further includes a second gas-liquid separator screen for filtering condensed amine liquid (lean liquid) mixed in the product gas.
Wherein the carbon dioxide with partial lean liquid (in the form of amine vapor) enters the condenser 163 via the evaporator first outlet 161B1 and the desorption gas condenser inlet 36A to be cooled, the cooled carbon dioxide with partial lean liquid enters the second gas-liquid separator 37 via the second gas-liquid separator inlet 37A, the carbon dioxide with partial lean liquid is separated into carbon dioxide product gas and lean liquid via the second gas-liquid separator 37 to be gas-liquid separated, and the carbon dioxide product gas is discharged via the second gas-liquid separator first outlet 37B1 to be subjected to the next operation.
The separated lean liquid is discharged through the second gas-liquid separator second outlet 37B2 and then refluxed into the absorbent reservoir 29 to be used as an absorbent.
The carbon dioxide with partial lean solution discharged from the desorption tower 17 is provided with a large amount of waste heat, the carbon dioxide with partial lean solution is subjected to heat exchange with the working medium in the heat pump system 16, so that the waste heat is effectively transferred to the working medium, and then the heat is transferred to the first path of rich solution which is separated by the rich solution splitter 14 through the working medium, the rich solution with heat absorption and temperature rise is desorbed in the desorption tower 17, the heat required by desorption is reduced, and the waste heat of gas at the top of the desorption tower 17 is effectively utilized; in addition, the lean liquid separated via the second gas-liquid separator 36 is returned to the absorbent reservoir 29 again, reducing the loss of lean liquid, and at the same time, the second gas-liquid separator captures at least part of lean liquid carried by the product gas with the arrangement of the screen, further reducing the loss of lean liquid.
Claims (9)
1. A chemical absorption carbon dioxide capture system based on waste heat recovery, comprising:
An absorption tower (11) comprising:
A first inlet (11A 1) of the absorption tower is positioned at the lower part of the absorption tower (11) and is used for allowing flue gas to enter, wherein the flue gas contains carbon dioxide;
a second inlet (11A 2) of the absorption tower, which is positioned at the upper part of the absorption tower (11) and is used for the absorbent to enter;
A first outlet (11B 1) of the absorption tower is positioned at the bottom of the absorption tower (11) and is used for flowing out the rich liquid;
a second outlet (11B 2) of the absorption tower, which is positioned at the top of the absorption tower (11);
A rich liquid pump (12) comprising:
A rich liquid pump inlet (12A) communicated with a first outlet (11B 1) of the absorption tower;
a rich liquid pump outlet (12B);
A first lean-rich liquid heat exchanger (13) comprising:
A first inlet (13A 1) of the first lean-rich liquid heat exchanger is communicated with an outlet (12B) of the rich liquid pump;
a first lean-rich liquid heat exchanger second inlet (13A 2);
a first outlet (13B 1) of the first lean-rich liquid heat exchanger;
a first lean-rich liquid heat exchanger second outlet (13B 2);
a rich liquid separator (14) comprising:
A rich liquid splitter inlet (14A) communicated with a first outlet (13B 1) of the first lean-rich liquid heat exchanger;
a rich liquid splitter first outlet (14B 1);
A rich liquor splitter second outlet (14B 2);
a second lean rich liquid heat exchanger (15) comprising:
a second lean-rich liquid heat exchanger first inlet (15A 1) communicated with a rich liquid splitter second outlet (14B 2);
a second lean rich liquid heat exchanger second inlet (15 A2);
a second lean-rich liquid heat exchanger first outlet (15B 1);
a second outlet (15B 2) of the second lean-rich liquid heat exchanger is communicated with a second inlet (13A 2) of the first lean-rich liquid heat exchanger;
a heat pump system (16) includes an evaporator (161), a compressor (162), a condenser (163), and a throttle valve (164),
An evaporator (161) comprising:
an evaporator first inlet (161 A1);
an evaporator second inlet (161 A2);
an evaporator first outlet (161B 1);
An evaporator second outlet (161B 2);
a compressor (162), comprising:
a compressor inlet (162A) communicating with the evaporator second outlet (161B 2);
a compressor outlet (162B);
a condenser (163) comprising:
A condenser first inlet (163A 1) communicating with the rich liquid splitter first outlet (14B 1);
A condenser second inlet (163 A2) in communication with the compressor outlet (162B);
a condenser first outlet (163B 1);
A condenser second outlet (163B 2);
A throttle valve (164) arranged between the condenser (163) and the evaporator (161), one end of which is controlled to be communicated with the second outlet (163B 2) of the condenser, and the other end of which is controlled to be communicated with the second inlet (161A 2) of the evaporator;
A desorption column (17) comprising:
A first inlet (17A 1) of the desorption tower is positioned at the upper part of the desorption tower (17) and is communicated with a first outlet (163B 1) of the condenser;
a second inlet (17A 2) of the desorption tower, which is positioned at the upper part of the desorption tower (17) and is lower than the first inlet (17A 1) of the desorption tower, and is communicated with a first outlet (15B 1) of the second lean-rich liquid heat exchanger;
a third inlet (17A 3) of the desorption tower, which is positioned in the middle of the desorption tower (17) and is lower than the second inlet (17A 2) of the desorption tower;
a fourth inlet (17A 4) of the desorption column, which is positioned at the lower part of the desorption column (17) and is lower than the third inlet (17A 3) of the desorption column;
a first outlet (17B 1) of the desorption tower is positioned at the top of the desorption tower (17) and is communicated with a first inlet (161A 1) of the evaporator;
A second outlet (17B 2) of the desorption tower is positioned at the bottom of the desorption tower (17);
a third outlet (17B 3) of the desorption tower, which is positioned at the lower part of the desorption tower (17);
a boiler (18) comprising:
A first inlet (18A 1) of the boiler is communicated with a third outlet (17B 3) of the desorption tower;
a boiler second inlet (18A 2) into which external saturated steam flows;
a boiler first outlet (18B 1) communicated with a fourth inlet (17A 4) of the desorption tower;
A boiler second outlet (18B 2);
lean liquid pump (19), comprising:
a lean solution pump inlet (19A) is communicated with a second outlet (13B 2) of the first lean solution heat exchanger;
a lean liquid pump outlet (19B);
A lean solution cooler (20), one side of which is communicated with a lean solution pump outlet (19B) and the other side of which is communicated with a second inlet (11A 2) of the absorption tower;
The flue gas enters the absorption tower (11) through the first inlet (11A 1) of the absorption tower and moves from bottom to top, the absorbent enters the absorption tower (11) through the second inlet (11A 2) of the absorption tower and sprays downwards, and the downwards sprayed absorbent contacts with the flue gas in a countercurrent way, so that the absorbent absorbs carbon dioxide in the flue gas to become rich liquid, the rich liquid is settled downwards, and the flue gas from which the carbon dioxide is removed continues to move upwards;
The rich liquid enters a rich liquid pump (12) through a first outlet (11B 1) of the absorption tower and a rich liquid pump inlet (12A), and then enters a first lean-rich liquid heat exchanger (13) through a rich liquid pump outlet (12B) and a first inlet (13A 1) of the first lean-rich liquid heat exchanger to perform first heat exchange so as to absorb heat and raise temperature;
the rich liquid after the first heat exchange enters the rich liquid splitter (14) through the first outlet (13B 1) of the first lean rich liquid heat exchanger and the inlet (14A) of the rich liquid splitter to split into two paths,
The first path of rich liquid enters the condenser (163) through the first outlet (14B 1) of the rich liquid splitter and the first inlet (163A 1) of the condenser to perform second heat exchange and absorb heat to raise temperature, and the first path of rich liquid after the second heat exchange enters the desorption tower (17) through the first outlet (163B 1) of the condenser and the first inlet (17A 1) of the desorption tower;
the second path of rich liquid enters the second lean and rich liquid heat exchanger (15) through a second outlet (14B 2) of the rich liquid splitter and a first inlet (15A 1) of the second lean and rich liquid heat exchanger to perform third heat exchange and absorb heat to raise temperature, and the second path of rich liquid after the third heat exchange is subjected to desorption tower (17) through a first outlet (15B 1) of the second lean and rich liquid heat exchanger and a second inlet (17A 2) of the desorption tower;
The first path of rich liquid and the second path of rich liquid are heated and desorbed in a desorption tower (17) and decomposed into lean liquid and carbon dioxide, the lean liquid is settled downwards in the desorption tower (17), and the carbon dioxide moves upwards;
Part of liquid at the bottom of the desorption tower (17) enters the boiler (18) through a third outlet (17B 3) of the desorption tower and a first inlet (18A 1) of the boiler, and carries out fourth heat exchange with saturated steam flowing in through a second inlet (18A 2) of the boiler, and the part of liquid absorbs heat in the boiler (18) and rises in temperature to be partially vaporized and enters the desorption tower (17) through the first outlet (18B 1) of the boiler and the fourth inlet (17A 4) of the desorption tower, so as to provide steam and heat for desorption of rich liquid in the desorption tower (17); the saturated steam in the boiler (18) is cooled by heat release and becomes condensed water, and the condensed water is discharged through a second outlet (18B 2) of the boiler;
The upward carbon dioxide carries partial lean liquid, then enters the evaporator (161) through a first outlet (17B 1) of the desorption tower and a first inlet (161A 1) of the evaporator, and performs heat absorption and temperature rise of the first rich liquid in the evaporator (161), the working liquid absorbs heat and changes into working medium steam, the working medium steam enters the compressor (162) through a second outlet (161B 2) of the evaporator and a compressor inlet (162A), the working medium steam is compressed by the compressor (162), the compressed working medium steam is changed into superheated steam through a second inlet (163A 2) of the condenser, the superheated steam enters the condenser (163) through a second outlet (162B) of the compressor, and performs heat absorption and temperature rise of the first rich liquid through the first inlet (163A 1) of the condenser, the superheated steam is changed into high-pressure working medium liquid through heat absorption and temperature drop of the first rich liquid, the high-pressure working medium liquid flows into a throttle valve (164) and is depressurized into liquid in an initial state, and the working medium liquid enters the evaporator (161) through the second inlet (161) of the evaporator under the action of a throttle valve (164) to finish the circulation process once again;
the lean solution desorbed from the desorption tower (17) enters the second lean-rich solution heat exchanger (15) through a second outlet (17B 2) of the desorption tower and a second inlet (15A 2) of the second lean-rich solution heat exchanger, and performs the third heat exchange with the second path of rich solution entering through a first inlet (15A 1) of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled;
The lean solution after the third heat exchange enters the first lean-rich solution heat exchanger (13) through a second outlet (15B 2) of the second lean-rich solution heat exchanger and a second inlet (13A 2) of the first lean-rich solution heat exchanger, performs the first heat exchange with the rich solution entering through a first inlet (13A 1) of the first lean-rich solution heat exchanger, releases heat for cooling, and enters the lean solution cooler (20) through a second outlet (13B 2) of the first lean-rich solution heat exchanger and a lean solution pump (19) after the first heat exchange, and then enters the absorber (11) through the lean solution cooler (20) and a second inlet (11A 2) of the absorber after the lean solution is cooled so as to be used as an absorbent for absorbing carbon dioxide.
2. The chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization according to claim 1, wherein,
The absorption tower (11) further comprises:
A third inlet (11A 3) of the absorption tower, which is positioned in the middle of the absorption tower (11) and below the second inlet (11A 2) of the absorption tower;
A third outlet (11B 3) of the absorption tower, which is positioned in the middle of the absorption tower (11) and above the third inlet (11A 3) of the absorption tower;
the chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises: an inter-stage cooler (21) one side of which is communicated with the third inlet (11A 3) of the absorption tower, and the other side of which is communicated with the third outlet (11B 3) of the absorption tower;
The absorbent in the absorption tower (11) flows into the inter-stage cooler (21) through the third outlet (11B 3) of the absorption tower to cool, the absorbent cooled through the inter-stage cooler (21) flows back into the absorption tower (11) through the third inlet (11A 3) of the absorption tower and sprays downwards, the downwards sprayed absorbent contacts with the flue gas entering through the first inlet (11A 1) of the absorption tower in a countercurrent way, and at least part of carbon dioxide in the flue gas is absorbed by the absorbent to become rich liquid, and the rich liquid is settled downwards; at least part of the carbon dioxide-removed flue gas continues to move upwards and is in countercurrent contact with the absorbent sprayed down through the second inlet (11A 2) of the absorption tower, the absorbent sprayed down through the second inlet (11A 2) of the absorption tower reacts for the second time to become rich liquid and carbon dioxide-removed flue gas, the generated rich liquid is settled downwards, the carbon dioxide-removed flue gas still continues to move upwards, and part of the absorbent is carried by the carbon dioxide-removed flue gas moving upwards.
3. The chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization according to claim 2, wherein,
The absorption tower (11) further comprises:
An absorber fourth inlet (11A 4) located at the upper part of the absorber (11) and located at the upper part of the absorber second inlet (11A 2);
a fourth outlet (11B 4) of the absorption tower, which is positioned at the upper part of the absorption tower (11) and above the second inlet (11A 2) of the absorption tower, and is used for the outflow of the pre-stored water washing water in the absorption tower (11);
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises:
A primary wash pump (22), comprising:
A primary washing pump inlet (22A) connected to the fourth outlet (11B 4) of the absorption column;
a primary wash pump outlet (22B);
A primary washing cooler (23), one side of which is connected to the primary washing pump outlet (22B), and the other side of which is connected to the fourth inlet (11A 4) of the absorption tower;
The absorption tower (11), the primary washing pump (22) and the primary washing cooler (23) form a primary washing loop, after the primary washing pump (22) is started, washing water in the absorption tower (11) flows into the primary washing pump (22) through a fourth outlet (11B 4) of the absorption tower and a primary washing pump inlet (22A), then flows into the primary washing cooler (23) through the primary washing pump outlet (22B) for cooling, cooled washing water flows back to the upper part of the absorption tower (11) again and is sprayed downwards, carbon dioxide is removed, flue gas carrying part of absorbent moves upwards in the absorption tower (11) and is contacted with cooled washing water in a countercurrent mode, at least part of absorbent in the flue gas is dissolved in the washing water, and the flue gas after primary washing continues to move upwards and is discharged through a second outlet (11B 2) of the absorption tower.
4. A chemical absorption process carbon dioxide capturing system based on waste heat recovery and utilization according to claim 3, wherein,
The flue gas discharged through the second outlet (11B 2) of the absorber also carries part of the absorbent;
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises:
a first gas-liquid separator (24), comprising:
A first gas-liquid separator inlet (24A) communicated with a second outlet (11B 2) of the absorption tower;
A first outlet (24B 1) of the first gas-liquid separator is positioned at the bottom of the first gas-liquid separator (24);
a first gas-liquid separator second outlet (24B 2) located at the top of the first gas-liquid separator (24);
A washing tower (25), wherein washing water is stored in the washing tower (25), and the washing tower (25) comprises:
A first inlet (25A 1) of the washing tower is positioned in the middle of the washing tower (25) and is communicated with a second outlet (24B 2) of the first gas-liquid separator;
a second inlet (25A 2) of the washing tower, which is positioned at the upper part of the washing tower (25);
a first outlet (25B 1) of the washing tower, which is positioned at the top of the washing tower (25);
a second outlet (25B 2) of the washing tower, which is positioned at the lower part of the washing tower (25);
a third outlet (25B 3) of the washing tower, which is positioned at the bottom of the washing tower (25);
A secondary wash pump (26), comprising:
A secondary washing pump inlet (26A) communicated with a second outlet (25B 2) of the washing tower;
a secondary wash pump outlet (26B);
A secondary washing cooler (27), one side of which is communicated with the outlet (26B) of the secondary washing pump, and the other side of which is communicated with the second inlet (25A 2) of the washing tower;
lean solution diverter (28), comprising:
A lean liquid splitter first inlet (28A 1) communicated with a first gas-liquid separator first outlet (24B 1);
A lean solution splitter second inlet (28A 2) communicated with a third outlet (25B 3) of the washing tower;
a lean liquid splitter outlet (28B);
An absorbent reservoir (29) comprising:
An absorber reservoir inlet (29A) in communication with a lean stream splitter outlet (28B);
an absorbent reservoir outlet (29B) communicating with one side of the lean solution cooler (20);
Wherein the flue gas which is discharged from the second outlet (11B 2) of the absorption tower and carries part of the absorbent enters the first gas-liquid separator (24) through the inlet (24A) of the first gas-liquid separator, the first gas-liquid separator (24) separates at least part of the absorbent from the flue gas,
The flue gas is discharged through a second outlet (24B 2) of the first gas-liquid separator, the discharged flue gas still contains at least part of absorbent, the flue gas containing at least part of absorbent enters the washing tower (25) through a first inlet (25A 1) of the washing tower and moves upwards, water washing water in the washing tower (25) enters the second washing pump (26) through a second outlet (25B 2) of the washing tower and a second washing pump inlet (26A), then flows into the second washing cooler (27) through a second outlet (26B) of the second washing pump to be cooled, the cooled water washing water enters the washing tower (25) through a second inlet (25A 2) of the washing tower and is sprayed downwards, water washing water sprayed downwards is in countercurrent contact with the flue gas carrying at least part of absorbent, the absorbent in the flue gas is dissolved by the water washing water, the flue gas with the absorbent removed is discharged through the first outlet (25B 1) of the washing tower, and the water washing water with the absorbent dissolved into the lean liquid (28A 2) flows into the lean liquid (28) through a third outlet (25B 3) of the washing tower;
The absorbent separated by the first gas-liquid separator (24) flows into the lean liquid separator (28) through the first gas-liquid separator first outlet (24B 1) and the lean liquid separator first inlet (28 A1);
the lean solution splitter (28) mixes the two paths of absorbent, the mixed absorbent enters the absorbent storage (29) through the lean solution splitter outlet (28B) and the absorbent storage (29) inlet, and then flows into the absorption tower (11) through the absorbent storage outlet (29B) and the lean solution cooler (20) to be recycled.
5. The waste heat recovery-based chemical absorption method carbon dioxide capturing system according to claim 1, further comprising:
A flash tank (30), comprising:
a flash tank inlet (30A) communicated with a second outlet (17B 2) of the desorption tower;
A flash tank first outlet (30B 1);
A flash tank second outlet (30B 2) communicating with a second lean-rich liquid heat exchanger second inlet (15 A2);
Roots blower (31), comprising:
a Roots blower inlet (31A) communicated with a flash tank first outlet (30B 1);
roots blower outlet (31B);
a steam cooler (32), one side of which is communicated with the Roots blower outlet (31B) and the other side of which is communicated with the third inlet (17A 3) of the desorption tower;
The lean solution flowing out from the second outlet (17B 2) of the desorption tower directly enters the flash tank (30) through the flash tank inlet (30A), the lean solution is flashed in the flash tank (30) to flash part of steam, the flash steam enters the Roots blower (31) through the first outlet (30B 1) of the flash tank and the Roots blower inlet (31A), the steam is pressurized and heated in the Roots blower (31), then enters the steam cooler (32) through the Roots blower outlet (31B) to be cooled, and the cooled steam enters the desorption tower (17) through the third inlet (17A 3) of the desorption tower to provide auxiliary heat for desorption of the rich solution in the desorption tower (17); the lean solution after the flash evaporation treatment enters the second lean-rich solution heat exchanger (15) through a second outlet (30B 2) of the flash evaporation tank and a second inlet (15A 2) of the second lean-rich solution heat exchanger, and performs the third heat exchange with the second rich solution entering through a first inlet (15A 1) of the second lean-rich solution heat exchanger, so that the lean solution releases heat and lowers the temperature.
6. The waste heat recovery-based chemical absorption method carbon dioxide capturing system according to claim 1, further comprising:
A purifying tower (33), wherein a purifying agent is stored in the purifying tower (33), and the purifying tower (33) comprises:
A first inlet (33A 1) of the purifying tower is positioned at the lower part of the purifying tower (33) for the external flue gas to enter;
a purifying column second inlet (33A 2) located at the upper part of the purifying column (33);
A first purifying tower outlet (33B 1) positioned at the top of the purifying tower (33) and communicated with a first absorbing tower inlet (11A 1);
a purification tower second outlet (33B 2) located at the lower part of the purification tower (33) and below the purification tower first inlet (33A 1);
a purge pump (34), comprising:
A purge pump inlet (34A) communicating with a purge column second outlet (33B 2);
A purge pump outlet (34B);
A purification cooler (35), one side of which is communicated with a purification pump outlet (34B) and the other side of which is communicated with a purification tower second inlet (33A 2);
Wherein the purification tower (33), the purification pump (34) and the purification cooler (35) form an external flue gas purification circulation loop, when the purification pump (34) is started, the purifying agent in the purification tower (33) is discharged through a second outlet (33B 2) of the purification tower, pumped into the purification cooler (35) through the purification pump (34) for cooling, and then returned into the purification tower (33) through a second inlet (33A 2) of the purification tower and sprayed downwards, external flue gas enters the purification tower (33) through a first inlet (33A 1) of the purification tower and moves upwards, the upwards moving external flue gas is in countercurrent contact with the purifying agent sprayed downwards through the second inlet (33A 2) of the purification tower, the purifying agent absorbs acidic impurity gas and smoke dust in the external flue gas, and carbon dioxide in the external flue gas is not absorbed by the purifying agent, and the flue gas moves upwards and enters the absorption tower (11) through the first outlet (33B 1) of the purification tower and the first inlet (11A 1) of the absorption tower so as to be supplied to the absorption tower (11).
7. The chemical absorption process carbon dioxide capturing system based on waste heat recovery and utilization according to claim 6, wherein,
The purifying agent is sodium bicarbonate solution.
8. The chemical absorption method carbon dioxide capturing system based on waste heat recovery and utilization according to claim 1, wherein,
The carbon dioxide discharged from the first outlet (17B 1) of the desorption column also carries part of the lean liquid;
The chemical absorption method carbon dioxide capturing system based on waste heat recycling also comprises:
jie Xiqi condenser (36) comprising:
Jie Xiqi a condenser inlet (36A) communicating with the evaporator first outlet (161B 1);
a desorber condenser outlet (36B);
A second gas-liquid separator (37) comprising:
A second gas-liquid separator inlet (37A) in communication with a stripping gas condenser outlet (36B);
a second gas-liquid separator first outlet (37B 1) located at the top of the second gas-liquid separator (37);
a second outlet (37B 2) of the second gas-liquid separator, which is positioned at the bottom of the second gas-liquid separator (37);
Wherein the carbon dioxide with partial lean liquid enters a condenser (163) for cooling through a first outlet (161B 1) of the evaporator and a desorption gas condenser inlet (36A), the cooled carbon dioxide with partial lean liquid enters a second gas-liquid separator (37) through a second gas-liquid separator inlet (37A), the carbon dioxide with partial lean liquid is separated into carbon dioxide product gas and lean liquid through the second gas-liquid separator (37) for gas-liquid separation, and the carbon dioxide product gas is discharged through a first outlet (37B 1) of the second gas-liquid separator for the next operation;
The separated lean liquid is discharged through a second outlet (37B 2) of the second gas-liquid separator and then refluxed into the absorbent reservoir (29).
9. The waste heat recovery based chemical absorption carbon dioxide capture system of claim 1, wherein the absorbent is an organic amine solution.
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| CN102527191A (en) * | 2010-11-17 | 2012-07-04 | 株式会社东芝 | Carbon dioxide recovery apparatus and carbon dioxide recovery method |
| CN104936678A (en) * | 2013-02-21 | 2015-09-23 | 三菱重工业株式会社 | System and method for recovering gas containing co2 and h2s |
| CN104338417A (en) * | 2013-07-29 | 2015-02-11 | 株式会社东芝 | Carbon dioxide separating and capturing system and method of operating same |
| CN103463955A (en) * | 2013-09-16 | 2013-12-25 | 湖南大学 | Technology for separating and recovering carbon dioxide from industrial tail gas |
| CN108744893A (en) * | 2018-07-12 | 2018-11-06 | 华中农业大学 | CO based on heat pipe intensified recuperation of heat2Chemical absorbing System and method for |
| CN208771134U (en) * | 2018-07-12 | 2019-04-23 | 华中农业大学 | CO2 chemical absorption system based on heat pipe enhanced heat recovery |
| CN108815993A (en) * | 2018-07-24 | 2018-11-16 | 中石化石油工程技术服务有限公司 | The carbon dioxide capture system utilized based on Waste Heat Recovery |
| CN210729090U (en) * | 2019-05-16 | 2020-06-12 | 中石化石油工程技术服务有限公司 | Chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization |
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