CN116251446A - High-temperature flue gas carbon dioxide capturing process and system - Google Patents
High-temperature flue gas carbon dioxide capturing process and system Download PDFInfo
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- CN116251446A CN116251446A CN202211728944.1A CN202211728944A CN116251446A CN 116251446 A CN116251446 A CN 116251446A CN 202211728944 A CN202211728944 A CN 202211728944A CN 116251446 A CN116251446 A CN 116251446A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 204
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 239000003546 flue gas Substances 0.000 title claims abstract description 114
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 102
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 102
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 44
- 238000003795 desorption Methods 0.000 claims abstract description 62
- 238000005057 refrigeration Methods 0.000 claims abstract description 50
- 239000000498 cooling water Substances 0.000 claims abstract description 48
- 238000001816 cooling Methods 0.000 claims abstract description 47
- 238000010521 absorption reaction Methods 0.000 claims abstract description 41
- 238000011084 recovery Methods 0.000 claims abstract description 29
- 238000009834 vaporization Methods 0.000 claims abstract description 24
- 230000008016 vaporization Effects 0.000 claims abstract description 24
- 238000007906 compression Methods 0.000 claims abstract description 21
- 230000006835 compression Effects 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 20
- 238000001704 evaporation Methods 0.000 claims abstract description 18
- 230000008020 evaporation Effects 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 238000010992 reflux Methods 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims description 140
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 66
- 239000011552 falling film Substances 0.000 claims description 14
- 239000010865 sewage Substances 0.000 claims description 13
- 239000002250 absorbent Substances 0.000 claims description 9
- 230000002745 absorbent Effects 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 18
- 230000008929 regeneration Effects 0.000 abstract description 17
- 238000011069 regeneration method Methods 0.000 abstract description 17
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 239000002918 waste heat Substances 0.000 abstract description 5
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000005507 spraying Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000006096 absorbing agent Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
- F22B3/04—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass by drop in pressure of high-pressure hot water within pressure-reducing chambers, e.g. in accumulators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- 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
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/50—Carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a high-temperature flue gas carbon dioxide capturing process and a high-temperature flue gas carbon dioxide capturing system, wherein the process and the system mainly comprise the parts of flue gas intake, heat recovery, purified flue gas emission, interstage cooling, distributed heat exchange-split desorption, lean solution evaporation and vaporization, lean solution throttling and vaporization compression, lean solution reflux, carbon dioxide recovery, heat pump refrigeration circulation, high-temperature steam heating, cooling water cooling and the like. The process and the system efficiently recycle the waste heat of high-temperature flue gas and desorption tower top gas, respectively promote forward reaction in the absorption tower and desorption reaction in the desorption tower, reduce the consumption of the cooling water of the steam at the top of the desorption tower, additionally generate low-grade steam, finally greatly reduce the regeneration energy consumption of the system, improve the comprehensive heat source utilization efficiency of the system, and realize the efficient capture and ultralow energy consumption operation of carbon dioxide.
Description
Technical Field
The invention belongs to the field of carbon peak carbon neutralization, and particularly relates to a high-temperature flue gas carbon dioxide capturing process and system.
Background
At present, available carbon capture technologies of coal-fired power plants mainly comprise a pre-combustion decarburization technology, a post-combustion decarburization technology and an oxygen-enriched combustion decarburization technology, and have the characteristics of the technologies for different technical routes. The carbon dioxide trapped and recovered in the coal-fired power plant can be injected into petroleum and natural gas fields to improve the oil gas recovery ratio, or injected into geological structures such as non-exploitation coal fields to be sealed and stored, and can also be widely used as an important industrial production raw material in the fields of metallurgy, steel, petroleum, chemical industry, electronics, food, medical treatment and the like.
CN114632402a provides a flue gas carbon dioxide capturing system and capturing method, which adopts two desorbers with different pressures, so that the rate of regeneration reaction is improved, the residence time required by rich liquor regeneration is reduced, and the carbon capturing operation cost and energy consumption are reduced. CN113385010a provides a flue gas carbon dioxide capturing system and capturing method for a power plant, which improves the capturing efficiency of carbon dioxide by performing regeneration treatment on reactants used for capturing. CN113171679a provides an integrated system and method for capturing and utilizing flue gas and carbon dioxide, which realizes the calcium circulation of the desulfurization system and effectively solves the problems of desulfurization raw material source and desulfurization waste disposal. CN114259837a provides a method for efficiently capturing carbon dioxide in flue gas, which adopts an adsorption tower to capture carbon dioxide in flue gas and uses hot steam for desorption treatment. CN111482069a provides an energy-saving flue gas carbon dioxide recovery system and recovery process, which integrates cooling, washing and absorption into one tower, and adopts staged regeneration, thereby saving the regeneration heat and flue gas cooling cold. CN110926108A provides a medium-low temperature industrial flue gas carbon dioxide trapping system, and adopts heat exchange, water removal, compression, precooling, back cooling and cryogenic flow to realize low-energy-consumption trapping of carbon dioxide in medium-low temperature industrial flue gas. The carbon dioxide capturing systems of all the above patents are completely different from the present invention, and do not mention the processes of heat recovery vapor compression, interstage cooling, distributed heat exchange, split flow desorption, lean solution throttling vaporization compression, heat pump refrigeration cycle, etc., and have obvious differences.
From the technical and economic point of view, the invention provides a high-temperature flue gas carbon dioxide capturing process and a high-temperature flue gas carbon dioxide capturing system, which can reduce the regeneration energy consumption of the system, improve the comprehensive heat source utilization efficiency of the system and realize the high-efficiency capturing and ultralow energy consumption operation of carbon dioxide by reducing the loss of the waste heat of the high-temperature flue gas; the method has good market prospect by reducing the cost of carbon dioxide capture of the coal-fired power plant, and simultaneously can generate important economic and social values for the current policies of carbon dioxide emission reduction, environmental protection and energy conservation.
Disclosure of Invention
First, the technical problem to be solved
The technical problems to be solved by the invention are as follows: overcomes the defects existing in the prior art, and provides a high-temperature flue gas carbon dioxide capturing process and a high-temperature flue gas carbon dioxide capturing system for reducing the waste heat loss of high-temperature flue gas and realizing the efficient capturing and ultralow energy consumption operation of carbon dioxide.
(II) technical scheme
In order to solve the technical problems, the technical scheme of the invention is as follows: a high-temperature flue gas carbon dioxide capturing process and system mainly comprise flue gas inlet, heat recovery, purified flue gas emission, interstage cooling, distributed heat exchange-split desorption, lean solution evaporation and vaporization, lean solution throttling and vaporization compression, lean solution backflow, carbon dioxide recovery, heat pump refrigeration cycle, high-temperature steam heating, cooling water cooling and the like;
the flue gas inlet and heat recovery part is connected and crossed with the first-stage flue gas heat exchanger (YQHR 01);
the flue gas inlet, the purified flue gas discharge, the interstage cooling, the distributed heat exchange-split desorption and the lean liquid reflux part are connected with each other and are intersected with an absorption tower (XST);
the distributed heat exchange-split flow desorption, lean solution evaporation and vaporization, lean solution throttling evaporation and compression and carbon dioxide recovery parts are connected with each other and are crossed with a desorption tower (JXT);
the lean solution evaporation and vaporization part is connected with the lean solution throttling and vaporization compression part and is intersected with the gas-liquid separator 3 (QYFL 03);
the lean liquid throttling vaporization compression part is connected with the lean liquid reflux part and is intersected with the flash tank 2 (SZG 02);
the lean liquid reflux and the distributed heat exchange-split desorption part are connected and are intersected with the lean-rich liquid heat exchanger 1 (PHHR 01) and the lean-rich liquid heat exchanger 2 (PHHR 02);
the carbon dioxide recovery part is connected with the heat pump refrigeration cycle part and is crossed with the refrigeration evaporator (ZZFQ);
the heat pump refrigeration cycle is connected with the distributed heat exchange-split flow desorption part and is crossed with a refrigeration condenser (ZLNQ);
the high-temperature steam heating part is connected with the lean liquid evaporation part and is crossed with a falling film reboiler (JMZQ);
the cooling water cooling and purifying smoke discharging part is connected and crossed with the cooler 3 (LQQ 03);
the cooling water is connected with the flue gas inlet part and is intersected with the three-stage flue gas heat exchanger (YQHR 03);
the cooling water cooling and carbon dioxide recovery part is connected and crossed with the cooler 4 (LQQ);
the cooling water cooling part is connected with the inter-stage cooling part and is intersected with the cooler 1 (LQQ);
the cooling water cooling and lean liquid reflux portion is connected and intersects with the cooler 2 (LQQ 02).
Further, the flue gas inlet part comprises high-temperature flue Gas (GWYQ), a primary flue gas heat exchanger (YQHR 01), a secondary flue gas heat exchanger (YQHR 02), a tertiary flue gas heat exchanger (YQHR 03), a centrifugal fan (LXFJ) and an absorption tower (XST) which are connected in sequence;
the high-temperature flue Gas (GWYQ) is from the high-temperature flue gas after desulfurization of the power plant;
the primary flue gas heat exchanger (YQHR 01) is used for heating the circulating water;
the secondary flue gas heat exchanger (YQHR 02) is used for preheating a carbon dioxide rich liquid at the bottom part of an absorption tower (XST);
the three-stage flue gas heat exchanger (YQHR 03) is used for cooling flue gas through cooling water;
the centrifugal fan (LXFJ) is used for sending the flue gas into the absorption tower (XST);
the absorber column (XST) is used to completely absorb carbon dioxide in the flue gas.
Further, the heat recovery part comprises a circulating water pump (XHSB), a primary flue gas heat exchanger (YQHR 01), a throttle valve 1 (JLF 01), a flash tank 1 (SZG 01), sewage drainage (WSPS), a water spraying Pump (PSB), a water vapor compressor 1 (SYSJ 01) and medium-temperature water vapor (ZWSZ) which are connected in sequence;
the circulating water pump (XHSB) is used for sending low-temperature liquid water into the primary flue gas heat exchanger (YQHR 01) for heating;
the throttle valve 1 (JLF 01) is used for throttling the high-temperature liquid water to evaporate and generate low-temperature steam;
the flash tank 1 (SZG 01) is used for storing and separating liquid water and low-temperature steam, and for performing sewage drainage (WSPS);
the water spraying Pump (PSB) is used for spraying water to the water vapor compressor 1 (SYSJ 01);
the water vapor compressor 1 (SYSJ 01) is used for compressing low temperature vapor from the flash tank 1 (SZG 01);
the medium-temperature water vapor (ZWSZ) is reused in other process sections.
Further, the purified flue gas discharging portion includes an absorption tower (XST), a cooler 3 (LQQ 03), a gas-liquid separator 1 (QYFL 01), a purified gas (JHQT), and condensed water drain (LNSP) connected in this order;
the cooler 3 (LQQ 03) is used for cooling and purifying the flue gas through cooling water;
the gas-liquid separator 1 (QYFL 01) is used for separating and purifying liquid water and non-condensing gas in the flue gas and performing condensed water drainage (LNSP);
the purified gas (JHQT) can be directly discharged into the atmosphere after reaching the standard.
Further, the interstage cooling part comprises an absorption tower (XST), a cooler 1 (LQQ) and an absorption tower (XST) which are connected in sequence;
the cooler 1 (LQQ 01) is used for inter-stage cooling by cooling water.
Further, the distributed heat exchange-split desorption part comprises an absorption tower (XST), a rich liquor pump (FYB) and a splitter 1 (FLQ 01) which are connected in sequence; one part of the flow divider 1 (FLQ 01) is sequentially connected with a secondary flue gas heat exchanger (YQHR 02) and a desorption tower (JXT), and the other part is sequentially connected with a lean rich liquid heat exchanger 1 (PHHR 01) and a flow divider 2 (FLQ 02); one part of the flow divider 2 (FLQ 02) is sequentially connected with a refrigeration condenser (ZLNQ) and a desorption tower (JXT), and the other part of the flow divider is sequentially connected with a lean rich liquid heat exchanger 2 (PHHR 02) and a desorption tower (JXT);
the bottom of the absorption tower (XST) can be used for sewage drainage (WSPS);
the rich liquid pump (FYB) is used for conveying the carbon dioxide rich liquid at the bottom of the absorption tower (XST);
the splitter 1 (FLQ 01) is used for splitting the carbon dioxide rich liquid once;
the desorber (JXT) is used to desorb carbon dioxide from the absorbent;
the lean-rich liquid heat exchanger 1 (PHHR 01) is used for carrying out primary preheating on the carbon dioxide rich liquid;
the splitter 2 (FLQ 02) is used for secondarily splitting the carbon dioxide rich liquid;
the refrigeration condenser (ZLNQ) is used for reheating the carbon dioxide rich liquid subjected to primary preheating;
the lean rich liquid heat exchanger 2 (PHHR 02) is used for carrying out secondary preheating on the carbon dioxide rich liquid which is subjected to primary preheating.
Further, the lean solution evaporation part comprises a desorption tower (JXT), a lean solution circulating pump 2 (PYXB 02), a reboiler circulating pump (ZFXB), a falling film reboiler (JMZQ), a gas-liquid separator 3 (QYFL 03) and a desorption tower (JXT) which are connected in sequence;
the bottom of the desorption column (JXT) can be subjected to sewage drainage (WSPS);
the lean solution circulating pump 2 (PYXB 02) is used for conveying carbon dioxide lean solution at the bottom of the desorption tower (JXT);
the reboiler circulation pump (ZFXB) is used for circulating and conveying the carbon dioxide lean liquid to the falling film reboiler (JMZQ);
the falling film reboiler (JMZQ) is used for heating the carbon dioxide lean liquid to generate vaporization to generate steam;
the gas-liquid separator 3 (QYFL 03) is used for separating water vapor and a liquid absorbent after evaporation and vaporization of the lean solution, and for performing wastewater drainage (WSPS).
Further, the lean solution throttling vaporization compression part comprises a gas-liquid separator 3 (QYFL 03), a lean solution circulating pump 1 (PYXB 01), a throttle valve 3 (JLF 03), a flash tank 2 (SZG 02), a water vapor compressor 2 (SYSJ 02) and a desorption tower (JXT) which are connected in sequence;
the lean solution circulating pump 1 (PYXB 01) is used for conveying the carbon dioxide lean solution in the gas-liquid separator 3 (QYFL 03);
the throttle valve 3 (JLF 03) is used for throttling the high-temperature carbon dioxide lean liquid to vaporize to generate low-temperature steam;
the flash tank 2 (SZG 02) is used for storing and separating liquid carbon dioxide lean liquid and low-temperature steam, and carrying out sewage drainage (WSPS);
the water vapor compressor 2 (SYSJ 02) is used to compress low temperature vapor from the flash tank 2 (SZG 02).
Further, the lean liquid reflux part comprises a flash tank 2 (SZG 02), a lean liquid Pump (PYB), a lean and rich liquid heat exchanger 2 (PHHR 02), a lean and rich liquid heat exchanger 1 (PHHR 01), a cooler 2 (LQQ 02), water, an absorbent (SXSJ) and an absorption tower (XST) which are connected in sequence;
the lean liquid Pump (PYB) is used for conveying the carbon dioxide lean liquid in the flash tank 2 (SZG 02) to reflux;
the cooler 2 (LQQ 02) is used for cooling the reflowed carbon dioxide lean liquid through cooling water;
the water and absorbent (SXSJ) are used to additionally supplement the absorption column (XST).
Further, the carbon dioxide recovery section includes a desorber (JXT), a refrigeration evaporator (ZZFQ), a cooler 4 (LQQ 04), a gas-liquid separator 2 (QYFL 02), crude carbon dioxide (EYHT), which are connected in this order;
the refrigeration evaporator (ZZFQ) is used for recovering heat of high-temperature gas at the top of the desorption tower (JXT);
said cooler 4 (LQQ 04) is used for cooling the steam entrained in the crude carbon dioxide (EYHT) by means of cooling water;
the gas-liquid separator 2 (QYFL 02) for separating liquid water and crude carbon dioxide (EYHT), and performing condensed water drainage (LNSP);
the crude carbon dioxide (EYHT) may be subjected to carbon dioxide utilization and sequestration.
Further, the heat pump refrigeration cycle part comprises a refrigeration evaporator (ZZFQ), a refrigeration compressor (ZYSJ), a refrigeration condenser (ZLNQ) and a throttle valve 2 (JLF 02) which are connected in sequence;
the refrigeration compressor (ZYSJ) is used for compressing steam from the refrigeration evaporator (ZZFQ);
the throttle valve 2 (JLF 02) is used for throttling the liquid refrigerant to evaporate and generate refrigeration cycle steam.
Further, the high-temperature steam heating part comprises high-temperature steam (GWZQ), a falling film reboiler (JMZQ) and condensate water drainage (LNSP) which are connected in sequence;
the high temperature steam (GWZQ) is used to heat a falling film reboiler (JMZQ).
Further, the cooling water inlet (LQSJ) of the cooling water cooling part is connected to the cooler 3 (LQQ), the three-stage flue gas heat exchanger (YQHR 03), the cooler 4 (LQQ 04), the cooler 1 (LQQ 01), and the cooler 2 (LQQ 02) respectively, and then connected to the cooling water outlet (LQSC).
(III) beneficial effects
After the technical scheme is adopted, the invention has the following beneficial effects:
(1) The process and the heat recovery part of the system efficiently recover the waste heat of the high-temperature flue gas, improve the utilization efficiency of a heat source and additionally generate low-grade water vapor;
(2) The inter-stage cooling part in the process and the system reduces the rich liquid temperature of the absorption tower, promotes the forward reaction in the absorption tower, increases the rich liquid carbon dioxide load, and further reduces the regeneration energy consumption of the system;
(3) The process and the distributed heat exchange and split flow desorption part in the system jointly improve the rich liquid temperature, promote the desorption reaction in the desorption tower, and reduce the regeneration energy consumption of the system;
(4) The process and the lean solution throttling vaporization compression part in the system improve the temperature of the lean solution flash steam, promote the desorption reaction of the rich solution and reduce the regeneration energy consumption of the system;
(5) The process and the system have the advantages that the heat of the high-temperature gas at the top of the desorption tower is efficiently recovered by the heat pump refrigeration cycle part, the rich liquid temperature is improved, the utilization efficiency of a heat source is improved, the consumption of the vapor cooling water at the top of the desorption tower is reduced, and the regeneration energy consumption of the system is reduced;
(6) Compared with other processes and systems, the process and the system greatly reduce the loss of the waste heat of the high-temperature flue gas, greatly reduce the regeneration energy consumption of the system, greatly improve the comprehensive heat source utilization efficiency of the system, and realize the efficient capture and ultralow energy consumption operation of the carbon dioxide.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 shows a process and a system for capturing carbon dioxide in high-temperature flue gas.
The symbols in the figures are respectively as follows:
high temperature flue Gas (GWYQ), primary flue gas heat exchanger (YQHR 01), secondary flue gas heat exchanger (YQHR 02), tertiary flue gas heat exchanger (YQHR 03), centrifugal fan (LXFJ), absorption tower (XST), cooler 3 (LQQ 03), gas-liquid separator 1 (QYFL 01), purge gas (JHQT), flash tank 1 (SZG 01), circulating water pump (XHSB), throttle valve 1 (JLF 01), steam compressor 1 (SYSJ 01), medium temperature water vapor (ZWSZ), water spray Pump (PSB), cooler 1 (LQQ 01), rich liquid pump (FYB), splitter 1 (FLQ 01), lean rich liquid heat exchanger 1 (PHHR 01), splitter 2 (FLQ 02) lean-rich liquid heat exchanger 2 (PHHR 02), desorber (JXT), cooler 4 (LQQ 04), gas-liquid separator 2 (QYFL 02), crude carbon dioxide (EYHT), refrigeration evaporator (zfq), refrigeration compressor (ZYSJ), refrigeration condenser (ZLNQ), throttle valve 2 (JLF 02), lean-liquid circulation pump 2 (PYXB 02), falling-film reboiler (JMZQ), gas-liquid separator 3 (QYFL 03), reboiler circulation pump (ZFXB), lean-liquid circulation pump 1 (PYXB 01), throttle valve 3 (JLF 03), flash tank 2 (SZG 02), steam compressor 2 (SYSJ 02), lean-liquid Pump (PYB), cooler 2 (LQQ 02), cooling water inlet (LQSJ), cooling water effluent (LQSC), water and absorbent (SXSJ), condensate drain (LNSP), high temperature water vapor (GWZQ), sewage drain (WSPS).
Detailed Description
In order that the invention may be more readily understood, a more particular description of the invention will be rendered by reference to specific embodiments that are illustrated in the appended drawings.
As shown in figure 1, the process and the system mainly comprise the parts of flue gas intake, heat recovery, purified flue gas emission, interstage cooling, distributed heat exchange-split desorption, lean solution evaporation and vaporization, lean solution throttling and vaporization compression, lean solution reflux, carbon dioxide recovery, heat pump refrigeration cycle, high-temperature steam heating, cooling water cooling and the like.
Preferably, as shown in fig. 1, the flue gas inlet part comprises a high-temperature flue Gas (GWYQ), a primary flue gas heat exchanger (YQHR 01), a secondary flue gas heat exchanger (YQHR 02), a tertiary flue gas heat exchanger (YQHR 03), a centrifugal fan (LXFJ) and an absorption tower (XST) which are connected in sequence;
the high temperature flue Gas (GWYQ) is from the high temperature flue gas after desulfurization in a power plant, and the temperature is typically about 170 ℃, and typically contains about 82% nitrogen, about 7% carbon dioxide, about 9% oxygen, and about 2% other gases;
the working flow of the flue gas inlet part is specifically as follows:
firstly, high-temperature flue Gas (GWYQ) from a power plant after desulfurization enters the cooling side of a primary flue gas heat exchanger (YQHR 01), and circulating water is heated through heat recovery of the high-temperature flue gas; secondly, cooling and then continuously entering a secondary flue gas heat exchanger (YQHR 02) and carrying out cooling and heat exchange on the carbon dioxide rich liquid from the bottom part of an absorption tower (XST); then, continuously entering a three-stage flue gas heat exchanger (YQHR 03) to perform cooling and cooling heat exchange with cooling water, and then flowing to a centrifugal fan (LXFJ); and finally, conveying the flue gas to a filler lower end inlet of an absorption tower (XST) through a centrifugal fan (LXFJ), thereby completing the working process of a flue gas inlet part.
Preferably, as shown in fig. 1, the heat recovery part includes a circulating water pump (XHSB), a primary flue gas heat exchanger (YQHR 01), a throttle valve 1 (JLF 01), a flash tank 1 (SZG 01), sewage drain (WSPS), a water spray Pump (PSB), a steam compressor 1 (SYSJ 01), and medium-temperature water vapor (ZWSZ) connected in this order;
the heat recovery part is mainly used for carrying out primary heat exchange on high-temperature flue gas by using circulating water, carrying out reduced pressure flash evaporation after passing through a throttle valve, and carrying out high-efficiency compression on steam generated by flash evaporation to provide medium-temperature water steam which can be applied to other related energy utilization production processes;
the workflow of the heat recovery part is specifically as follows:
firstly, cooling water inflow (LQSJ) enters a flash tank 1 (SZG 01), and liquid water at the bottom is conveyed to the liquid side of a primary flue gas heat exchanger (YQHR 01) for heating through a circulating water pump (XHSB); secondly, high-temperature liquid water from the primary flue gas heat exchanger (YQHR 01) is throttled by a throttle valve 1 (JLF) to be gasified to generate low-temperature steam, and the gas-liquid mixture reenters a flash tank 1 (SZG 01) for gas-liquid separation; then, the low-temperature steam at the top of the flash tank 1 (SZG 01) enters the steam compressor 1 (SYSJ 01) for mechanical compression, so that the steam temperature is increased; at the same time, liquid water from the flash tank 1 (SZG 01) is delivered to the water vapor compressor 1 (SYSJ 01) for spraying water through a water spraying Pump (PSB); further, the flash tank 1 (SZG 01) may perform sewage drainage (WSPS); and finally, storing the compressed medium-temperature water vapor (ZWSZ) and recycling the medium-temperature water vapor to other process sections, thereby completing the working process of the heat recovery part.
Preferably, as shown in fig. 1, the purified flue gas discharging section includes an absorption tower (XST), a cooler 3 (LQQ 03), a gas-liquid separator 1 (QYFL 01), a purified gas (JHQT), and condensed water drain (LNSP) connected in this order;
the working flow of the fume emission purification part is specifically as follows:
firstly, flue gas entering from the lower end of a filler of an absorption tower (XST) gradually flows to the top of the tower from bottom to top, and is fully contacted with liquid reflowed by an inter-stage cooling part, so that the absorption of carbon dioxide in the flue gas is enhanced; fully contacting the waste gas with liquid reflowed by the lean liquid reflow part to fully absorb carbon dioxide in the flue gas; secondly, the flue gas coming out of the top of the absorption tower (XST) enters a cooler 3 (LQQ) to condense the entrained steam by cooling water, and then enters a gas-liquid separator 1 (QYFL 01) to perform gas-liquid separator, and the gas-liquid separator 1 (QYFL 01) can also perform condensate water drainage (LNSP); finally, the purified gas (JHQT) coming out from the top of the gas-liquid separator 1 (QYFL 01) can be directly discharged into the atmosphere after reaching the standard, thereby completing the working process of purifying the fume discharge part.
Preferably, as shown in FIG. 1, the interstage cooling section comprises an absorber column (XST), a cooler 1 (LQQ), an absorber column (XST) connected in sequence;
the interstage cooling part is mainly introduced by using a cooler 1 (LQQ 01) to reduce the rich liquid temperature of the absorption tower, reduce the reaction temperature to promote the forward reaction in the absorption tower, increase the carbon dioxide load of the rich liquid and further reduce the regeneration energy consumption of the system;
the work flow of the interstage cooling part is specifically as follows:
firstly, gas from the middle part of an absorption tower (XST) enters the gas side of a cooler 1 (LQQ), is cooled by cooling water, and then flows back to the lower port of the middle part of the absorption tower (XST); next, the cooling water inlet water (LQSJ) enters the liquid side of the cooler 1 (LQQ 01) and flows to the cooling water outlet water (LQSC), thereby completing the operation of the inter-stage cooling section.
Preferably, as shown in fig. 1, the distributed heat exchange-split desorption section includes an absorption column (XST), a rich liquor pump (FYB), and a splitter 1 (FLQ 01) connected in sequence; one part of the flow divider 1 (FLQ 01) is sequentially connected with a secondary flue gas heat exchanger (YQHR 02) and a desorption tower (JXT), and the other part is sequentially connected with a lean rich liquid heat exchanger 1 (PHHR 01) and a flow divider 2 (FLQ 02); one part of the flow divider 2 (FLQ 02) is sequentially connected with a refrigeration condenser (ZLNQ) and a desorption tower (JXT), and the other part of the flow divider is sequentially connected with a lean rich liquid heat exchanger 2 (PHHR 02) and a desorption tower (JXT);
the distributed heat exchange part is mainly introduced by utilizing two lean-rich liquid heat exchangers connected in series to improve the temperature of rich liquid, promote the desorption reaction in a desorption tower, reduce the regeneration energy consumption of the system, and the distributed heat exchange is generally combined with split-flow desorption;
the split-flow desorption part is mainly used for splitting the rich liquid by using a splitter, one part of split-flow rich liquid enters a lean-rich liquid heat exchanger 1 (PHHR 01), one part of split-flow rich liquid enters a lean-rich liquid heat exchanger 2 (PHHR 02), the other part of split-flow rich liquid exchanges heat with a refrigeration condenser (ZLNQ), and the two parts can enable the rich liquid to reach higher temperature; the other part of the split cold rich liquid enters a secondary flue gas heat exchanger (YQHR 02) so as to enable the rich liquid to reach higher temperature, and finally, the regeneration energy consumption of the system is comprehensively reduced; the flow of the hot rich liquid is reduced after the flow division, so that the temperature of the hot rich liquid is higher, and the desorption reaction in the desorption tower is more facilitated;
the work flow of the distributed heat exchange-split desorption part is specifically as follows:
firstly, sewage drainage (WSPS) can be carried out at the bottom of an absorption tower (XST), and carbon dioxide rich liquid from the bottom of the absorption tower (XST) is conveyed to a splitter 1 (FLQ 01) for primary split flow through a rich liquid pump (FYB); secondly, a part of carbon dioxide rich liquid of the flow divider 1 (FLQ 01) flows to the liquid side of the secondary flue gas heat exchanger (YQHR 02) for primary preheating, and enters the top of a desorption tower (JXT) for backflow after the temperature is increased; thirdly, after the other part of the carbon dioxide rich liquid of the splitter 1 (FLQ 01) flows to the heating side of the lean-rich liquid heat exchanger 1 (PHHR 01) for preheating, the carbon dioxide rich liquid continuously enters the splitter 2 (FLQ 02) for secondary splitting; then, part of the carbon dioxide rich liquid of the flow divider 2 (FLQ 02) flows to a refrigeration condenser (ZLNQ), and directly enters the top of a desorption tower (JXT) for backflow after being preheated; finally, the other part of the carbon dioxide rich liquid of the splitter 2 (FLQ 02) enters the heating side of the lean-rich liquid heat exchanger 2 (PHHR 02) to be subjected to secondary preheating, and then enters the middle part of the desorption tower (JXT) to be subjected to reflux, so that the working process of the distributed heat exchange-split flow desorption part is completed.
Preferably, as shown in fig. 1, the lean solution evaporation and vaporization part includes a desorption column (JXT), a lean solution circulating pump 2 (PYXB 02), a reboiler circulating pump (ZFXB), a falling film reboiler (JMZQ), a gas-liquid separator 3 (QYFL 03), and a desorption column (JXT) connected in this order;
the working flow of the lean liquid evaporation part is specifically as follows:
firstly, sewage drainage (WSPS) can be carried out at the bottom of a desorption tower (JXT), and carbon dioxide lean solution coming out of the bottom of the desorption tower (JXT) is conveyed to the top of a falling film reboiler (JMZQ) through a lean solution circulating pump 2 (PYXB 02); secondly, gasifying the heated carbon dioxide lean solution, then, separating gas and liquid in a gas-liquid separator 3 (QYFL 03), and conveying a part of the carbon dioxide lean solution to a reboiler circulating pump (ZFXB) to the top of a falling film reboiler (JMZQ) again to complete continuous circulating conveying; finally, the gas-liquid separator 3 (QYFL 03) can perform sewage drainage (WSPS), and steam coming out from the top of the gas-liquid separator 3 (QYFL 03) enters the middle of the desorption tower (JXT) to flow from bottom to top, so that the working process of the lean solution evaporation part is completed.
Preferably, as shown in fig. 1, the lean solution throttling vaporization compression part comprises a gas-liquid separator 3 (QYFL 03), a lean solution circulating pump 1 (PYXB 01), a throttle valve 3 (JLF 03), a flash tank 2 (SZG 02), a water vapor compressor 2 (SYSJ 02) and a desorption tower (JXT) which are connected in sequence;
the lean solution throttling vaporization compression part is mainly introduced by utilizing lean solution flash evaporation pressurization, the pressurized flash evaporation gas enters a desorption tower and is contacted with rich solution to exchange heat and condense to release a large amount of heat, and the heat can promote the desorption reaction of the rich solution and reduce the regeneration energy consumption of a system;
the working flow of the lean solution throttling vaporization compression part is specifically as follows:
firstly, carbon dioxide lean solution coming out of the bottom of a gas-liquid separator 3 (QYFL 03) is conveyed into a throttle valve 3 (JLF) through a lean solution circulating pump 1 (PYXB 01) to be throttled and vaporized to generate low-temperature steam, and then flows into a flash tank 2 (SZG 02); secondly, the flash tank 2 (SZG 02) can carry out sewage drainage (WSPS), and low-temperature steam coming out from the top of the flash tank 2 (SZG 02) is mechanically compressed by the steam compressor 2 (SYSJ 02) to generate superheated steam; finally, the compressed superheated steam enters the bottom of a desorption tower (JXT) to flow from bottom to top, thereby completing the working process of the lean solution throttling vaporization compression part.
Preferably, as shown in fig. 1, the lean liquid reflux part comprises a flash tank 2 (SZG 02), a lean liquid Pump (PYB), a lean-rich liquid heat exchanger 2 (PHHR 02), a lean-rich liquid heat exchanger 1 (PHHR 01), a cooler 2 (LQQ 02), water and absorbent (SXSJ), and an absorption tower (XST) which are connected in sequence;
the working flow of the lean liquid reflux part is specifically as follows:
firstly, carbon dioxide lean solution coming out of the bottom of a flash tank 2 (SZG 02) is conveyed to the cooling side of a lean-rich solution heat exchanger 2 (PHHR 02) through a lean solution Pump (PYB), and then enters the cooling side of a lean-rich solution heat exchanger 1 (PHHR 01) for continuous cooling; next, the carbon dioxide lean liquid coming out of the cooling side of the lean-rich liquid heat exchanger 1 (PHHR 01) is fed into the cooler 2 (LQQ 02) together with additional supplementary water and absorbent (SXSJ), and the back-flowing carbon dioxide lean liquid is cooled by the cooling water; finally, the lean solution enters the top of the absorption tower (XST) from the cooler 2 (LQQ 02) to reflux from top to bottom, so that the working process of the lean solution reflux part is completed.
Preferably, as shown in fig. 1, the carbon dioxide recovery section includes a desorber (JXT), a refrigeration evaporator (ZZFQ), a cooler 4 (LQQ 04), a gas-liquid separator 2 (QYFL 02), crude carbon dioxide (EYHT), which are connected in this order;
the working flow of carbon dioxide recovery is specifically as follows:
first, the crude carbon dioxide (EYHT) desorbed from the top of the desorber (JXT) enters a refrigeration evaporator (ZZFQ) to recover the heat of the high temperature gas at the top of the desorber (JXT), and then enters a cooler 4 (LQQ) to continue cooling the steam entrained in the crude carbon dioxide (EYHT) by cooling water; secondly, the gas is discharged from the cooler 4 (LQQ 04) and then enters the gas-liquid separator 2 (QYFL 02) for gas-liquid separation, and the separated gas is the final crude carbon dioxide (EYHT) which can be used for carbon dioxide utilization and sealing; finally, the gas-liquid separator 2 (QYFL 02) may perform condensate water drainage (LNSP), thereby completing the operation of the carbon dioxide recovery section.
Preferably, as shown in fig. 1, the heat pump refrigeration cycle part includes a refrigeration evaporator (ZZFQ), a refrigeration compressor (ZYSJ), a refrigeration condenser (ZLNQ), a throttle valve 2 (JLF 02) connected in this order;
the heat pump refrigeration cycle part is mainly introduced by utilizing a compression type heat pump system to recycle the heat of high-temperature gas at the top of a desorption tower (JXT), after the heat is firstly subjected to heat exchange with a heat pump working medium, the heat is subjected to temperature rise and pressure rise through a refrigeration compressor (ZYSJ), and then enters a refrigeration condenser (ZLNQ) to exchange heat with rich liquid subjected to heat exchange from a lean-rich liquid heat exchanger 1 (PHHR 01), so that the rich liquid reaches higher temperature, thereby not only reducing the consumption of steam cooling water at the top of the desorption tower, but also reducing the regeneration energy consumption of the system;
the working flow of the heat pump refrigeration cycle part is specifically as follows:
firstly, steam from a refrigeration evaporator (ZZFQ) enters a refrigeration compressor (ZYSJ) for compression, and then enters a refrigeration condenser (ZLNQ) for secondary preheating of a part of carbon dioxide rich liquid from a splitter 2 (FLQ 02); secondly, the gaseous refrigerant is condensed into liquid refrigerant, and enters a throttle valve 2 (JLF 02) to be throttled and vaporized to regenerate refrigeration cycle steam; finally, the regenerated refrigeration cycle steam enters a refrigeration compressor (ZYSJ) to be compressed, thereby completing the working process of the refrigeration cycle part of the heat pump.
Preferably, as shown in fig. 1, the high temperature steam heating part includes high temperature steam (GWZQ), a falling film reboiler (JMZQ), and condensed water drain (LNSP) connected in this order;
the working flow of the high-temperature steam heating part is specifically as follows:
first, high-temperature water vapor (GWZQ) enters a falling film reboiler (JMZQ) in two ways, and the circulating liquid is heated to evaporate; secondly, the high-temperature steam (GWZQ) is heated and then condensed to generate condensed water, and condensed water drainage (LNSP) is carried out, so that the working process of the high-temperature steam heating part is completed.
Preferably, as shown in fig. 1, the cooling water inlet (LQSJ) of the cooling water cooling part is connected to the cooler 3 (LQQ 03), the three-stage flue gas heat exchanger (YQHR 03), the cooler 4 (LQQ 04), the cooler 1 (LQQ 01), and the cooler 2 (LQQ 02), and then is connected to the cooling water outlet (LQSC);
the working flow of the cooling water cooling part is specifically as follows:
firstly, part of cooling water inflow (LQSJ) enters a cooler 3 (LQQ) to cool flue gas coming out of the top of an absorption tower (XST), and then cooling water outflow (LQSC) is carried out; secondly, part of cooling water inflow (LQSJ) enters a three-stage flue gas heat exchanger (YQHR 03) to cool and exchange heat to flue gas, and then cooling water outflow (LQSC) is carried out; thirdly, part of the cooling water inflow (LQSJ) enters a cooler 4 (LQQ) to continuously cool the crude carbon dioxide (EYHT) desorbed from the top of the desorption tower (JXT), and then cooling water outflow (LQSC) is carried out; then, part of the cooling water inflow (LQSJ) enters a cooler 1 (LQQ) to interstage cool the steam from the middle part of the absorption tower (XST), and then the cooling water outflow (LQSC) is carried out; finally, a part of the cooling water inflow (LQSJ) enters the cooler 2 (LQQ 02) to cool the carbon dioxide lean solution coming out of the cooling side of the lean-rich solution heat exchanger 1 (PHHR 01) and the additional supplementary water and absorbent (SXSJ), and then the cooling water outflow (LQSC) is carried out, so that the working process of the cooling water cooling part is completed.
The technical problems, technical solutions and advantageous effects solved by the present invention have been further described in detail in the above-described embodiments, and it should be understood that the above-described embodiments are only illustrative of the present invention and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements, etc. within the spirit and principle of the present invention should be included in the scope of protection of the present invention.
Claims (13)
1. A high-temperature flue gas carbon dioxide capturing process and system are characterized by mainly comprising the following parts of flue gas intake, heat recovery, purified flue gas emission, interstage cooling, distributed heat exchange-split desorption, lean solution evaporation and vaporization, lean solution throttling and vaporization compression, lean solution reflux, carbon dioxide recovery, heat pump refrigeration cycle, high-temperature steam heating, cooling water cooling and the like.
2. The high-temperature flue gas carbon dioxide capturing process and system according to claim 1, wherein the flue gas inlet part comprises a high-temperature flue Gas (GWYQ), a primary flue gas heat exchanger (YQHR 01), a secondary flue gas heat exchanger (YQHR 02), a tertiary flue gas heat exchanger (YQHR 03), a centrifugal fan (LXFJ) and an absorption tower (XST) which are sequentially connected.
3. The process and system for capturing carbon dioxide in high temperature flue gas according to claim 2, wherein the heat recovery part comprises a circulating water pump (XHSB), a primary flue gas heat exchanger (YQHR 01), a throttle valve 1 (JLF), a flash tank 1 (SZG 01), sewage drain (WSPS), a water spray Pump (PSB), a steam compressor 1 (SYSJ 01), and medium temperature water vapor (ZWSZ) which are connected in sequence.
4. A high temperature flue gas carbon dioxide capturing process and system according to claim 3, wherein the purified flue gas discharging section comprises an absorption tower (XST), a cooler 3 (LQQ), a gas-liquid separator 1 (QYFL 01), a purified gas (JHQT), and condensed water drain (LNSP) which are connected in this order.
5. The process and system for capturing carbon dioxide from flue gas at a high temperature according to claim 4, wherein said inter-stage cooling section comprises an absorption tower (XST), a cooler 1 (LQQ) and an absorption tower (XST) connected in this order.
6. The process and system for capturing carbon dioxide in high temperature flue gas according to claim 5, wherein the distributed heat exchange-split desorption section comprises an absorption tower (XST), a rich liquor pump (FYB) and a splitter 1 (FLQ 01) which are connected in sequence; one part of the flow divider 1 (FLQ 01) is sequentially connected with a secondary flue gas heat exchanger (YQHR 02) and a desorption tower (JXT), and the other part is sequentially connected with a lean rich liquid heat exchanger 1 (PHHR 01) and a flow divider 2 (FLQ 02); one part of the splitter 2 (FLQ 02) is sequentially connected with a refrigeration condenser (ZLNQ) and a desorption tower (JXT), and the other part is sequentially connected with a lean rich liquid heat exchanger 2 (PHHR 02) and a desorption tower (JXT).
7. The process and system for capturing carbon dioxide in flue gas at high temperature according to claim 6, wherein the lean solution evaporation and vaporization section comprises a desorber (JXT), a lean solution circulating pump 2 (PYXB 02), a reboiler circulating pump (ZFXB), a falling film reboiler (JMZQ), a gas-liquid separator 3 (QYFL 03), and a desorber (JXT) which are sequentially connected.
8. The process and system for capturing carbon dioxide in high temperature flue gas according to claim 7, wherein the lean solution throttling vaporization compression section comprises a gas-liquid separator 3 (QYFL 03), a lean solution circulating pump 1 (PYXB 01), a throttle valve 3 (JLF 03), a flash tank 2 (SZG 02), a vapor compressor 2 (SYSJ 02), and a desorber (JXT) which are sequentially connected.
9. The process and system according to claim 8, wherein the lean liquid reflux portion comprises a flash tank 2 (SZG 02), a lean liquid Pump (PYB), a lean rich liquid heat exchanger 2 (PHHR 02), a lean rich liquid heat exchanger 1 (PHHR 01), a cooler 2 (LQQ 02), water and absorbent (SXSJ), and an absorption tower (XST) connected in sequence.
10. The process and system for capturing carbon dioxide from flue gas at high temperature according to claim 9, wherein the carbon dioxide recovery section comprises a desorber (JXT), a refrigeration evaporator (ZZFQ), a cooler 4 (LQQ), a gas-liquid separator 2 (QYFL 02), and crude carbon dioxide (EYHT) connected in this order.
11. The high temperature flue gas carbon dioxide capturing process and system according to claim 10, wherein the heat pump refrigeration cycle part comprises a refrigeration evaporator (ZZFQ), a refrigeration compressor (ZYSJ), a refrigeration condenser (ZLNQ), and a throttle valve 2 (JLF 02) which are connected in sequence.
12. The high temperature flue gas carbon dioxide capturing process and system according to claim 11, wherein the high temperature steam heating section comprises high temperature steam (GWZQ), falling film reboiler (JMZQ), condensed water drain (LNSP) connected in order.
13. The process and system according to claim 12, wherein the cooling water inlet (LQSJ) of the cooling water cooling part is connected to the cooler 3 (LQQ), the three-stage flue gas heat exchanger (YQHR 03), the cooler 4 (LQQ), the cooler 1 (LQQ) and the cooler 2 (LQQ 02), respectively, and then is connected to the cooling water outlet (LQSC).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118022490A (en) * | 2024-01-11 | 2024-05-14 | 浙江省环保集团生态环保研究院有限公司 | Novel low-pressure flue gas CO2Energy-saving trapping process |
| CN118687405A (en) * | 2024-08-26 | 2024-09-24 | 泰兴市南磷化工有限公司 | Heat energy recovery device for phosphoric acid production |
-
2022
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118022490A (en) * | 2024-01-11 | 2024-05-14 | 浙江省环保集团生态环保研究院有限公司 | Novel low-pressure flue gas CO2Energy-saving trapping process |
| CN118022490B (en) * | 2024-01-11 | 2024-10-01 | 浙江省环保集团生态环保研究院有限公司 | Low-pressure flue gas CO2Energy-saving trapping process |
| CN118687405A (en) * | 2024-08-26 | 2024-09-24 | 泰兴市南磷化工有限公司 | Heat energy recovery device for phosphoric acid production |
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