CN117504584A - Flue gas NO X Removal and CO 2 System and method for capturing and cooperatively combining - Google Patents
Flue gas NO X Removal and CO 2 System and method for capturing and cooperatively combining Download PDFInfo
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- CN117504584A CN117504584A CN202311851790.XA CN202311851790A CN117504584A CN 117504584 A CN117504584 A CN 117504584A CN 202311851790 A CN202311851790 A CN 202311851790A CN 117504584 A CN117504584 A CN 117504584A
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- flue gas
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- absorption tower
- removal
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 239000003546 flue gas Substances 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 124
- 239000007788 liquid Substances 0.000 claims abstract description 115
- 238000010521 absorption reaction Methods 0.000 claims abstract description 79
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 62
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 62
- 239000007789 gas Substances 0.000 claims abstract description 42
- 230000003197 catalytic effect Effects 0.000 claims abstract description 37
- 238000003421 catalytic decomposition reaction Methods 0.000 claims abstract description 30
- 238000011069 regeneration method Methods 0.000 claims abstract description 27
- 230000008929 regeneration Effects 0.000 claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 238000007906 compression Methods 0.000 claims description 14
- 230000006835 compression Effects 0.000 claims description 12
- 239000011885 synergistic combination Substances 0.000 claims description 9
- 150000001412 amines Chemical class 0.000 claims description 6
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 229910044991 metal oxide Inorganic materials 0.000 claims description 4
- 150000004706 metal oxides Chemical group 0.000 claims description 4
- 230000008878 coupling Effects 0.000 claims description 3
- 238000010168 coupling process Methods 0.000 claims description 3
- 238000005859 coupling reaction Methods 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 84
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 20
- 229910021529 ammonia Inorganic materials 0.000 abstract description 10
- 239000003638 chemical reducing agent Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 238000004821 distillation Methods 0.000 abstract description 3
- 230000010354 integration Effects 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 2
- 239000010812 mixed waste Substances 0.000 abstract 1
- 239000010865 sewage Substances 0.000 abstract 1
- 239000002912 waste gas Substances 0.000 abstract 1
- 238000005406 washing Methods 0.000 description 12
- 239000012530 fluid Substances 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 238000007599 discharging Methods 0.000 description 5
- LXQMHOKEXZETKB-UHFFFAOYSA-N 1-amino-2-methylpropan-2-ol Chemical compound CC(C)(O)CN LXQMHOKEXZETKB-UHFFFAOYSA-N 0.000 description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 4
- NDVLTYZPCACLMA-UHFFFAOYSA-N silver oxide Chemical compound [O-2].[Ag+].[Ag+] NDVLTYZPCACLMA-UHFFFAOYSA-N 0.000 description 4
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 3
- SVYKKECYCPFKGB-UHFFFAOYSA-N N,N-dimethylcyclohexylamine Chemical compound CN(C)C1CCCCC1 SVYKKECYCPFKGB-UHFFFAOYSA-N 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 229910000420 cerium oxide Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 3
- 229960001124 trientine Drugs 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- LVMBEXJKZGJYRH-UHFFFAOYSA-N [Ag].[Ce] Chemical compound [Ag].[Ce] LVMBEXJKZGJYRH-UHFFFAOYSA-N 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229940031098 ethanolamine Drugs 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229910001923 silver oxide Inorganic materials 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 2
- BFSVOASYOCHEOV-UHFFFAOYSA-N 2-diethylaminoethanol Chemical compound CCN(CC)CCO BFSVOASYOCHEOV-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 1
- 239000005751 Copper oxide Substances 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- WYCDUUBJSAUXFS-UHFFFAOYSA-N [Mn].[Ce] Chemical compound [Mn].[Ce] WYCDUUBJSAUXFS-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- LHIJANUOQQMGNT-UHFFFAOYSA-N aminoethylethanolamine Chemical compound NCCNCCO LHIJANUOQQMGNT-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910000431 copper oxide Inorganic materials 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 1
- 229910001887 tin oxide Inorganic materials 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- 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
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention relates to the field of waste gas purification, and provides a flue gas NO for solving the problems that in the prior art, an additional SCR denitration reducing agent is required to be added and the energy consumption is high in a process for cooperatively removing nitrogen oxides and carbon dioxide x Removal and CO 2 The system comprises a catalytic denitration unit provided with a flue gas inlet, a catalytic decomposition unit, an absorption tower and a regeneration tower, wherein a flue gas heat exchanger is arranged between the catalytic denitration unit and the absorption tower, and a lean-rich liquid heat exchanger is arranged between the absorption tower and the regeneration tower. The system utilizes CO 2 The nitrogen oxide is removed by the organic vapor mixed waste gas discharged by the trapping system, so that pollution control by using sewage is realized, and meanwhileThe nitrogen oxide and the organic vapor are removed, the pollutant emission is controlled, the cost is reduced, and the CO is saved 2 An organic vapor recovery device in the trapping system and an ammonia distillation device of the denitration system; and the heat integration of the system is performed through flue gas heat exchange and waste heat recovery, so that the waste heat utilization of the system is realized, and the energy consumption is reduced.
Description
Technical Field
The invention relates to the technical field of industrial boiler flue gas purification, in particular to a flue gas NO x Removal and CO 2 A system and method for synergistic combination of trapping.
Background
Manmade carbon dioxide (CO) 2 ) The increased gas emission in isothermal chambers is a major cause of global climate change, and industrial boilers such as coal-fired power plants are a major large-scale fixed CO 2 An emission source. CO 2 Trapping technology is an essential technical route to achieve the goal of carbon neutralization. Nitrogen Oxides (NO) in industrial boiler flue gas x ) Is one of main pollutants causing photochemical smog, acid rain and haze, and has great potential hazard to human beings. Selective Catalytic Reduction (SCR) utilizes ammonia to reduce nitrogen oxides (NOx) to nitrogen (N) 2 ) The method is the most widely applied technology at present, and has the advantages of high denitration efficiency, small ammonia escape, safety, reliability and the like. However, the matched ammonia distillation equipment and ammonia source storage equipment of the SCR system are expensive, so that the application of the SCR system is limited. If the flue gas treatment system can automatically supply the SCR reducing agent, the construction cost of the SCR system can be greatly saved.
In recent years, researchers at home and abroad propose a process system and a method for cooperatively removing nitrogen oxides and carbon dioxide.As CN112044261A discloses a method for capturing CO 2 Method for CO-removing NO by utilizing reducing gases (CO and H) generated by biomass pyrolysis 2 、C x H y ) Reducing NO, absorbing CO by using calcium-based absorbent such as limestone, dolomite and the like 2 . However, under the technology, the biomass is easy to be mixed with O in the flue gas 2 The reaction has less yield of reducing gas and huge biomass consumption, and the process is carried out at 600-725 ℃, so that the energy consumption for maintaining the temperature is high, and the energy conservation is not facilitated. CN104162358A discloses a method for synchronously denitrating coal-fired flue gas and reducing emission and capturing carbon dioxide, which reduces nitrogen oxides by charcoal at high temperature (745 ℃), separates carbon dioxide at normal temperature, and reduces carbon dioxide into carbon monoxide by heating to 950 ℃. However, the operation temperature of the denitration and decarbonization method is extremely high, the heat recovery and the utilization are difficult, and the carbon is easy to deflagrate, so that the reagent industry is difficult to apply. CN105944526A discloses desulfurization and decarbonization at low temperature (35-70 ℃) of residual ammonia water produced by coking by NaClO 2 /H 2 O 2 The composite solution is subjected to denitration (70-105 ℃). However, this method uses ammonia to decarbonize, due to CO 2 The absorption rate is slow, CO 2 The trapping efficiency is low, the volatility of ammonia water is extremely high, the ammonia emission is easy to be serious, and the chemical solution NaClO 2 /H 2 O 2 The consumption is large and the cost is high. Meanwhile, the prior patent needs to input additional SCR denitration reducing agents (such as biomass, carbon, ammonia water and the like) and matched equipment, and has high reaction temperature, so that the system operation and investment cost are high.
Disclosure of Invention
The invention provides a flue gas NO for solving the problems that in the prior art, an additional SCR denitration reducing agent is required to be added and the required energy consumption is high in a process for cooperatively removing nitrogen oxides and carbon dioxide x Removal and CO 2 System for gathering and cooperatively using, which can be used for denitration of flue gas and gathering CO in flue gas 2 By coupling flue gas denitration and CO 2 And the trapping system realizes the waste heat utilization and the pollutant cooperative removal of the system through heat integration. The invention also provides a smoke NO x Removal and CO 2 Of the synergistic combination of trappingThe method does not need to use an additional SCR denitration reducing agent, and is environment-friendly and safe.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
flue gas NO x Removal and CO 2 A system for synergistic combinations of traps comprising
A catalytic denitration unit provided with a flue gas inlet;
the bottom air outlet of the catalytic decomposition unit is connected with the top of the catalytic denitration unit;
the gas inlet at the bottom of the absorption tower is connected with the gas outlet at the bottom of the catalytic denitration unit through a flue gas heat exchanger, and the gas outlet at the top of the absorption tower is connected with the gas inlet at the top of the catalytic decomposition unit through a flue gas heat exchanger;
the regeneration tower is provided with a low-temperature section and a high-temperature section which are connected from top to bottom, a liquid inlet of the low-temperature section is connected with a liquid outlet at the bottom of the absorption tower, the low temperature Duan Dingbu is a regenerated gas outlet, a liquid inlet of the high-temperature section is connected with a liquid outlet at the bottom of the absorption tower through a lean-rich liquid heat exchanger, and a liquid outlet at the bottom of the high-temperature section is connected with a liquid inlet at the top of the absorption tower through a lean-rich liquid heat exchanger.
The flue gas entering the catalytic denitration device contains ammonia, hydrocarbon and absorbent. The nitrogen oxide, oxygen, ammonia, hydrocarbon and absorbent are partially oxidized and decomposed into micromolecular reducing gas, then the micromolecular reducing gas reacts under the action of a denitration catalyst in a catalytic denitration unit to generate nitrogen and water, the purified mixed gas is discharged through a flue gas outlet, enters a flue gas heat exchanger for cooling, and then enters an absorption tower for removing carbon dioxide in the flue gas. The absorption liquid in the absorption tower fully absorbs carbon dioxide and then enters the lean-rich liquid heat exchanger to provide heat energy for carbon dioxide regeneration, then enters the regeneration tower to remove carbon dioxide and complete the regeneration of the absorption liquid, the regenerated absorption liquid enters the absorption tower again after passing through the lean-rich liquid heat exchanger to circularly absorb carbon dioxide, and the carbon dioxide removed from the regeneration tower is the carbon dioxide regenerated gas with high purity.
Preferably, the system further comprises a pretreatment tower, wherein the pretreatment tower is arranged between an air inlet at the bottom of the absorption tower and the flue gas heat exchanger, the air inlet at the bottom of the pretreatment tower is connected with the flue gas heat exchanger, and an air outlet at the top of the pretreatment tower is connected with the air inlet at the bottom of the absorption tower.
The pretreatment tower can further reduce the temperature of the flue gas after denitration, and is convenient for absorbing and capturing the subsequent carbon dioxide.
Preferably, a circulating pipeline is further arranged outside the pretreatment tower, the circulating pipeline is connected with the bottom and the top of the pretreatment tower, and a cooling device is arranged on the circulating pipeline.
Preferably, the system further comprises a water scrubber, wherein an air inlet at the bottom of the water scrubber is connected with an air outlet at the top of the absorption tower, a liquid outlet at the bottom of the water scrubber is connected with a liquid inlet at the top of the absorption tower, and an emptying port is arranged at the top of the water scrubber.
Preferably, the lean-rich liquid heat exchanger is a plate heat exchanger or a shell-and-tube heat exchanger.
Preferably, the liquid outlet at the bottom of the high-temperature section is also connected with the liquid inlet at the middle part of the high-temperature section through a reboiler.
The reboiler can further raise the temperature of the rich liquid after absorbing carbon dioxide, so that the carbon dioxide contained in the rich liquid is fully desorbed.
Preferably, the regenerated gas outlet is connected with a condenser, and the liquid outlet of the condenser is connected with the liquid inlet of the low-temperature section.
The condenser can remove the absorption liquid carried in the carbon dioxide regeneration gas, improve the concentration of carbon dioxide in the carbon dioxide regeneration gas, and return the absorption liquid to the regeneration tower.
Preferably, the outlet of the condenser is connected with the compression device, and the liquid outlet of the compression device is connected with the liquid inlet of the low-temperature section.
The compression device can further reduce the content of the absorption liquid in the carbon dioxide regeneration gas, and the carbon dioxide regeneration gas is convenient to transport. The regenerated gas can be separated into high-purity carbon dioxide through a condenser and a compression tower.
Preferably, a liquid outlet at the bottom of the water washing tower is connected with a liquid inlet at the top of the water washing tower through a cooling device.
The temperature reducing device can control the temperature of the washing liquid, and the overhigh temperature is avoided.
Preferably, the catalyst of the catalytic decomposition unit is a metal oxide catalyst, and the catalyst used in the catalytic denitration unit is a metal oxide catalyst.
Preferably, the catalyst of the catalytic decomposition unit is one or more of silver oxide, manganese oxide, cerium oxide, iron oxide, copper oxide and aluminum oxide; the catalyst used in the catalytic denitration unit is one or more of cerium oxide, manganese oxide, tin oxide, magnesium oxide, ferric oxide, titanium oxide and zirconium oxide.
Preferably, a heater is further arranged between the flue gas heat exchanger and the air inlet at the top of the catalytic decomposition unit.
Preferably, the absorption liquid in the absorption tower is an aqueous solution of organic amine, and the mass concentration of the organic amine is 30% -80%.
The aqueous solution of the organic amine has a good effect of capturing carbon dioxide and is easily catalytically decomposed into a low molecular weight reducing gas.
Preferably, the organic amine is one of ethanolamine, 1-amino-2-methyl-2-propanol, a mixture of 1-amino-2-methyl-2-propanol and piperazine, a mixture of hydroxyethyl ethylenediamine and diethylaminoethanol, and a mixture of triethylene tetramine and N, N-dimethylcyclohexylamine.
Flue gas NO x Removal and CO 2 The method for trapping and cooperatively combining uses the flue gas NO x Removal and CO 2 A system for capturing cooperative coupling comprising the steps of:
(1) Enabling the flue gas to enter a catalytic denitration unit from a flue gas inlet, and keeping the temperature of a catalytic decomposition unit at 150-600 ℃ and the temperature of the catalytic denitration unit at 120-600 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 30-50 ℃ in the reaction process, the flue gas accounting for 10-80% of the mass of the total flue gas is controlled to enter a catalytic decomposition device, and the residual flue gas after the reaction is emptied;
(3) And (3) enabling 0-15% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section to obtain carbon dioxide regenerated gas and lean liquid, controlling the temperature of the low temperature section of the regeneration tower to be 70-100 ℃, controlling the temperature of the high temperature section to be 100-150 ℃, and enabling the lean liquid to enter the absorption tower as absorption liquid again after heat exchange.
Therefore, the invention has the following beneficial effects: (1) by CO 2 The mixed exhaust gas of the organic vapor discharged by the trapping system is used for removing the nitrogen oxides, so that pollution control by using pollution is realized, the nitrogen oxides and the organic vapor are removed, the pollutant discharge is controlled, the cost is reduced, and meanwhile, CO is saved 2 The organic vapor recovery device in the trapping system and the ammonia distillation device of the denitration system provide enough space for upgrading and reforming the existing device; (2) and the heat integration of the system is performed through flue gas heat exchange and waste heat recovery, so that the waste heat utilization of the system is realized, and the energy consumption is reduced.
Drawings
Fig. 1 is a schematic structural diagram of embodiment 1.
The device comprises a 1-catalytic denitration unit, a 2-catalytic decomposition unit, a 3-absorption tower, a 4-flue gas heat exchanger, a 5-regeneration tower, a 6-lean-rich liquid heat exchanger, a 7-pretreatment tower, an 8-water washing tower, a 9-reboiler, a 10-condenser and an 11-compression device.
Description of the embodiments
The invention is further described below in connection with the detailed description and the accompanying drawings.
Example 1
Flue gas NO x Removal and CO 2 The system for the synergistic combination of trapping is shown in fig. 1, and comprises a catalytic denitration unit 1, a catalytic decomposition unit 2, a flue gas heat exchanger 3, an absorption tower 2, a lean-rich liquid heat exchanger 5 and a regeneration tower 3. The catalytic denitration device comprises a catalytic denitration unit 1 and a catalytic decomposition unit 2, wherein a flue gas inlet is formed in the top of the catalytic denitration unit 1, the catalytic denitration unit 1 is 1.5 m high with the diameter of 0.6 m, and 0.2m is placed in the catalytic denitration unit 1 3 The alumina-supported manganese cerium catalyst of (2) the catalytic decomposition unit 2 is a cylinder with the diameter of 0.6 meter and the height of 3 meters, and 0.45 m is placed in the catalytic decomposition unit 2 3 The top of the silver cerium catalyst loaded by alumina is provided with an air inlet, the bottom of the silver cerium catalyst is provided with an air outlet, and the air outlet is communicated with the top of the catalytic denitration unit 1. The diameter of the absorption tower 2 is 0.18 m and the height is 3 m, the top of the absorption tower is provided with an absorption liquid inlet, and the absorption liquid is absorbedThe liquid is ethanol amine with the content of 50 weight percent; the diameter of the regeneration tower 3 is 0.15 meter and the height is 3 meters, the upper part of the regeneration tower is a low-temperature section with the length of 0.9 meter, and the lower part of the regeneration tower is a high-temperature section with the low temperature Duan Liantong; the gas outlet at the bottom of the catalytic denitration unit 1 is connected with the gas inlet at the bottom of the absorption tower 2 through a hot fluid channel of the flue gas heat exchanger 3 and the pretreatment tower 7. The diameter of the pretreatment tower 7 is 0.2m and the height is 0.8 m, the bottom of the pretreatment tower 7 is provided with an air inlet, the top is provided with an air outlet, the side face of the pretreatment tower 7 is provided with a circulating pipeline, the circulating inlet of the circulating pipeline is close to the top of the pretreatment tower 7, the circulating outlet is close to the bottom of the pretreatment tower 7, and a cooling device is arranged in the circulating pipeline. The gas outlet at the top of the absorption tower 2 is sequentially connected with a cold fluid channel of the flue gas heat exchanger 3 and a gas inlet at the top of the catalytic decomposition unit 2, and a heater is arranged on a pipeline between the outlet of the cold fluid channel of the flue gas heat exchanger 3 and the gas inlet at the top of the catalytic decomposition unit 2; the liquid outlet pipeline at the bottom of the absorption tower 2 is divided into two paths, one path is connected with the liquid inlet at the upper part of the low-temperature section, and the other path is connected with the cold fluid channel inlet of the lean-rich liquid heat exchanger 5. The outlet of the cold fluid channel of the lean-rich liquid heat exchanger 5 is connected with the liquid inlet at the top of the high-temperature section through a pipeline, the pipeline at the liquid outlet at the bottom of the high-temperature section is divided into two paths, one path is connected with the liquid inlet arranged at the side surface of the high-temperature section near the bottom through a reboiler 9, and the other path is connected with the liquid inlet arranged at the side surface of the absorption tower 2 near the top through the hot fluid channel of the lean-rich liquid heat exchanger 5. The top of the absorption tower 2 is provided with an air outlet, the air outlet is connected with an air inlet at the bottom of a water washing tower 7, the diameter of the water washing tower 8 is 0.2m and 0.8 m, the top of the water washing tower 8 is an emptying port for discharging flue gas after denitration and decarbonation, a liquid outlet is arranged on the side surface of the water washing tower 8 near the bottom, the liquid outlet is connected with a liquid inlet on the top of the side surface of the water washing tower 6 through a heating device, and the liquid outlet is also connected with a liquid inlet on the side surface of the absorption tower 2 near the top. The low temperature Duan Dingbu of the regeneration tower 5 is a regenerated gas outlet, the regenerated gas outlet is connected with the inlet of the condenser 10, the outlet of the condenser 10 is connected with the inlet of the compression device 11 through a pipeline, and the liquid outlet of the condenser 10 and the liquid outlet of the compression device 11 are connected with the liquid inlet at the upper part of the low temperature section, so that condensed liquid of the regenerated gas in the condensation and compression process flows back into the low temperature section.
Example 2
Flue gas NO x Removal and CO 2 The system in which the trapping was cooperatively used was different from example 1 in that the water scrubber 6 and the reboiler 9 were not contained.
Example 3
Flue gas NO x Removal and CO 2 The system of the synergistic combination of trapping is different from example 1 in that the catalytic denitration unit 1 is placed with 0.2m 3 The catalyst composite of cerium oxide and titanium oxide is placed in 0.45. 0.45 m in the catalytic decomposition unit 2 3 Silver oxide catalyst of (2); the absorption liquid in the absorption tower is an aqueous solution of triethylene tetramine and N, N-dimethylcyclohexylamine, the mass concentration of the triethylene tetramine is 40%, and the mass concentration of the N, N-dimethylcyclohexylamine is 40%.
Example 4
Flue gas NO x Removal and CO 2 The flue gas is treated by a trapping and synergistic combination method, wherein the flue gas contains 360ppm of nitrogen oxides, and the initial temperature is 120 ℃;
the procedure used the apparatus described in example 1 was as follows:
(1) Enabling the flue gas to enter a catalytic denitration device from a flue gas inlet at a flow rate of 800L/h, and keeping the temperature of a catalytic decomposition unit at 300 ℃ and the temperature of the catalytic denitration unit at 240 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 50 ℃ in the reaction process, so that flue gas with the total mass of 30% of the flue gas enters a catalytic decomposition device, and the residual flue gas after the reaction is emptied after being treated by a water washing tower;
(3) And (3) enabling 90% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section, controlling a reboiler to enable the temperature of the high temperature section to be 100 ℃, enabling the temperature of the low temperature section to be 80 ℃, obtaining carbon dioxide regenerated gas and lean liquid, enabling the lean liquid to enter the absorption tower again as absorption liquid after heat exchange, and discharging the carbon dioxide regenerated gas after condensation and compression treatment.
Example 5
Flue gas NO x Removal and CO 2 Method for treating flue gas by combining trapping and co-operation, wherein the flue gas contains nitrogen oxides 200pThe pm initial temperature is 130 ℃;
the procedure used the apparatus described in example 1 was as follows:
(1) Enabling the flue gas to enter the catalytic denitration device from a flue gas inlet in the middle of the catalytic denitration device, and keeping the temperature of the catalytic decomposition unit at 400 ℃ and the temperature of the catalytic denitration unit at 220 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 40 ℃ in the reaction process, so that flue gas with 25% of total flue gas mass is subjected to residual reaction in a catalytic decomposition device, and the flue gas is subjected to treatment in a water washing tower and is then emptied;
(3) And (3) enabling 95% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section, controlling a reboiler to enable the temperature of the high temperature section to be 105 ℃ and the temperature of the low temperature section to be 85 ℃ to obtain carbon dioxide regenerated gas and lean liquid, enabling the lean liquid to be used as absorption liquid again after heat exchange and enter the absorption tower, and discharging the carbon dioxide regenerated gas after condensation and compression treatment.
Example 6
Flue gas NO x Removal and CO 2 The flue gas is treated by a method of trapping and cooperative combination, wherein the flue gas contains 280ppm of nitrogen oxides, and the initial temperature is 120 ℃;
the procedure used the apparatus described in example 2 was as follows:
(1) Enabling the flue gas to enter the catalytic denitration device from a flue gas inlet in the middle of the catalytic denitration device, and keeping the temperature of the catalytic decomposition unit at 400 ℃ and the temperature of the catalytic denitration unit at 220 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 40 ℃ in the reaction process, so that flue gas accounting for 25% of the total mass of the flue gas enters a catalytic decomposition device, and the residual flue gas after the reaction is directly emptied;
(3) And (3) enabling 95% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section, enabling the temperature of the high temperature section to be 101 ℃ and the temperature of the low temperature section to be 83 ℃ without opening a reboiler, obtaining carbon dioxide regenerated gas and lean liquid, enabling the lean liquid to enter the absorption tower again as absorption liquid after heat exchange, and discharging the carbon dioxide regenerated gas after condensation and compression treatment.
Example 7
Flue gas NO x Removal and CO 2 The flue gas is treated by a trapping and synergistic combination method, wherein the initial temperature of 400ppm of nitrogen oxides in the flue gas is 110 ℃;
the procedure used the apparatus described in example 3 was as follows:
(1) Enabling the flue gas to enter the catalytic denitration device from a flue gas inlet in the middle of the catalytic denitration device at a flow rate of 800L/h, and keeping the temperature of the catalytic decomposition unit at 300 ℃ and the temperature of the catalytic denitration unit at 240 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 50 ℃ in the reaction process, so that flue gas with the total mass of 30% of the flue gas enters a catalytic decomposition device, and the residual flue gas after the reaction is emptied after being treated by a water washing tower;
(3) And (3) enabling 90% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section, controlling a reboiler to enable the temperature of the high temperature section to be 100 ℃, enabling the temperature of the low temperature section to be 80 ℃, obtaining carbon dioxide regenerated gas and lean liquid, enabling the lean liquid to enter the absorption tower again as absorption liquid after heat exchange, and discharging the carbon dioxide regenerated gas after condensation and compression treatment.
The nitrogen oxide content in the flue gas exhausted from the water scrubber, the concentration of the carbon dioxide regenerated gas and the yield are respectively detected, and the results are shown in table 1.
TABLE 1
As shown in Table 1, the invention has good denitration effect on flue gas, and can collect and recycle carbon dioxide in the flue gas.
Claims (10)
1. Flue gas NO x Removal and CO 2 A system for collecting and cooperating combination is characterized by comprising
A catalytic denitration unit (1) provided with a flue gas inlet;
the bottom air outlet of the catalytic decomposition unit (2) is connected with the top of the catalytic denitration unit;
an air inlet at the bottom of the absorption tower is connected with an air outlet at the bottom of the catalytic denitration unit through a flue gas heat exchanger (4), and an air outlet at the top of the absorption tower is connected with an air inlet at the top of the catalytic decomposition unit through the flue gas heat exchanger;
the regeneration tower (5) comprises a low-temperature section and a high-temperature section which are connected from top to bottom, wherein a liquid inlet of the low-temperature section is connected with a liquid outlet at the bottom of the absorption tower, the low temperature Duan Dingbu is a regenerated gas outlet, a liquid inlet of the high-temperature section is connected with a liquid outlet at the bottom of the absorption tower through a lean-rich liquid heat exchanger (6), and a liquid outlet at the bottom of the high-temperature section is connected with a liquid inlet at the top of the absorption tower through a lean-rich liquid heat exchanger.
2. A flue gas NO according to claim 1 x Removal and CO 2 The system for capturing and cooperatively combining is characterized by further comprising a pretreatment tower (7), wherein the pretreatment tower is arranged between an air inlet at the bottom of the absorption tower and the flue gas heat exchanger, the air inlet at the bottom of the pretreatment tower is connected with the flue gas heat exchanger, and an air outlet at the top of the pretreatment tower is connected with the air inlet at the bottom of the absorption tower.
3. A flue gas NO according to claim 1 x Removal and CO 2 The system is characterized by further comprising a water scrubber (8), wherein an air inlet at the bottom of the water scrubber is connected with an air outlet at the top of the absorption tower, a liquid outlet at the bottom of the water scrubber is connected with a liquid inlet at the top of the absorption tower, and an emptying port is arranged at the top of the water scrubber.
4. A flue gas NO according to claim 1 x Removal and CO 2 The system for capturing and cooperatively using is characterized in that a liquid outlet at the bottom of the high-temperature section is also connected with a liquid inlet at the middle part of the high-temperature section through a reboiler (9).
5. A flue gas NO according to claim 1 x Removal and CO 2 Trapping aidThe combined system is characterized in that the regenerated gas outlet is connected with a condenser (10), and the liquid outlet of the condenser is connected with the liquid inlet of the low-temperature section.
6. A flue gas NO according to claim 5 x Removal and CO 2 The system for capturing and cooperatively utilizing is characterized in that an outlet of the condenser is connected with a compression device (11), and a liquid outlet of the compression device is connected with a liquid inlet of the low-temperature section.
7. A flue gas NO according to claim 1 x Removal and CO 2 The system for capturing and cooperatively combining is characterized in that the catalyst of the catalytic decomposition unit is a metal oxide catalyst, and the catalyst used by the catalytic denitration unit is a metal oxide catalyst.
8. A flue gas NO according to claim 1 or 7 x Removal and CO 2 The system for capturing and cooperatively utilizing the flue gas is characterized in that a heater is further arranged between the flue gas heat exchanger and an air inlet at the top of the catalytic decomposition unit.
9. A flue gas NO according to claim 1 x Removal and CO 2 The system for the synergistic combination of trapping is characterized in that absorption liquid in the absorption tower is aqueous solution of organic amine, and the mass concentration of the organic amine is 30% -80%.
10. Flue gas NO x Removal and CO 2 A method for the synergistic combination of trapping and using the flue gas NO according to any one of claims 1 to 9 x Removal and CO 2 A system for capturing cooperative coupling comprising the steps of:
(1) Enabling the flue gas to enter a catalytic denitration unit from a flue gas inlet, and keeping the temperature of a catalytic decomposition unit at 150-600 ℃ and the temperature of the catalytic denitration unit at 120-600 ℃;
(2) The flue gas after denitration enters an absorption tower through heat exchange and reacts with absorption liquid to obtain rich liquid, the temperature of the absorption tower is controlled to be 30-50 ℃ in the reaction process, the flue gas accounting for 10-80% of the mass of the total flue gas is controlled to enter a catalytic decomposition device, and the residual flue gas after the reaction is emptied;
(3) And (3) enabling 0-15% of the rich liquid to enter a high temperature section of the regeneration tower after heat exchange, enabling the rest rich liquid to enter a low temperature section to obtain carbon dioxide regenerated gas and lean liquid, controlling the temperature of the low temperature section of the regeneration tower to be 70-100 ℃, controlling the temperature of the high temperature section to be 100-150 ℃, and enabling the lean liquid to enter the absorption tower as absorption liquid again after heat exchange.
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