CN111841066B - System and method for removing acid gas in flue gas - Google Patents
System and method for removing acid gas in flue gas Download PDFInfo
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- CN111841066B CN111841066B CN202010820823.4A CN202010820823A CN111841066B CN 111841066 B CN111841066 B CN 111841066B CN 202010820823 A CN202010820823 A CN 202010820823A CN 111841066 B CN111841066 B CN 111841066B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 150
- 239000003546 flue gas Substances 0.000 title claims abstract description 150
- 239000007789 gas Substances 0.000 title claims abstract description 31
- 239000002253 acid Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000001179 sorption measurement Methods 0.000 claims abstract description 94
- 238000001035 drying Methods 0.000 claims abstract description 86
- 238000001816 cooling Methods 0.000 claims abstract description 79
- 239000000110 cooling liquid Substances 0.000 claims abstract description 38
- 239000002351 wastewater Substances 0.000 claims abstract description 8
- 239000000428 dust Substances 0.000 claims description 25
- 238000000746 purification Methods 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- 239000000741 silica gel Substances 0.000 claims description 5
- 229910002027 silica gel Inorganic materials 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 238000004065 wastewater treatment Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 abstract description 5
- 239000003463 adsorbent Substances 0.000 abstract description 2
- 239000002274 desiccant Substances 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract 2
- 230000001172 regenerating effect Effects 0.000 abstract 2
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000005406 washing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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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
- B01D53/002—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 condensation
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
-
- 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
- B01D53/26—Drying gases or vapours
-
- 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
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/30—Sorption devices using carbon, e.g. coke
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a system and a method for removing acid gas in flue gas, which are used for integrally removing acid gas components in coal-fired flue gas, dehydrating and cooling the flue gas through a cooling tower, intensively recycling the removed wastewater to realize zero emission of wastewater, recovering high-temperature flue gas heat while reducing the temperature of the flue gas through heat exchange between a high-temperature flue gas cooler and air, heating, dehydrating and regenerating a drying agent in a drying tower through medium-temperature air, heating and regenerating an adsorbent in an adsorption tower, fully recycling the high-temperature flue gas heat, recovering cold energy of low-temperature flue gas from the top of the adsorption tower through a cold energy recoverer, cooling a cooling liquid again, arranging the adsorption tower under a low-temperature working condition, absorbing the acid gas in the flue gas at one time, and having small initial investment, saving occupied land and no secondary pollution.
Description
Technical Field
The invention belongs to the technical field of flue gas pollutant purification, and particularly relates to a system and a method for removing acid gas in flue gas.
Background
The utilization mode of direct combustion of coal can generate a large amount of acid waste gas pollutants, such as smoke dust, SO 2, NOx and the like, which seriously influence the balance of ecological environment and the physical health of people. The main component of NOx is NO, and also contains a small amount of NO 2. At present, the mainstream flue gas purification technology adopts the combination of SCR denitration, ESP electric precipitation and FGD wet desulfurization to carry out desulfurization and denitration and dust removal.
The traditional flue gas desulfurization and denitration adopts a separate treatment method, and has the disadvantages of huge equipment, complex technology and high cost although certain results are achieved, thus greatly influencing the development of a thermal power plant. For example, FGD wet desulfurization technology occupies a large area, needs a large amount of limestone as an auxiliary absorbent, and has the disadvantages of easy corrosion and scaling of the inner wall of equipment and high maintenance difficulty. The SCR denitration technology has high initial investment cost, needs to continuously consume ammonia or urea as a reducing agent, and has the advantages of easy poisoning and failure of an SCR catalyst, high treatment difficulty and high operation cost. Therefore, the research of a novel and efficient flue gas desulfurization and denitrification technology becomes a focus of researchers at home and abroad.
Disclosure of Invention
The invention aims to provide a system and a method for removing acid gas in flue gas, which overcome the defects of the prior art, and can simultaneously remove the acid gas in the coal-fired flue gas, and the system and the method have the advantages of high removal efficiency, low operation cost and easy maintenance of a device.
In order to achieve the above purpose, the invention adopts the following technical scheme:
The system for removing the acid gas in the flue gas comprises a high-temperature flue gas cooler, a No. 1 fan, a dust remover, a cooling tower, a cooling circulating pump, a cooler, a cold quantity recoverer, a drying tower, a cooling unit, a sub-cooling cooler, an adsorption tower and a No. 2 fan;
The flue gas inlet of the high-temperature flue gas cooler is connected to the high-temperature flue gas outlet of the power plant air preheater, the flue gas outlet of the high-temperature flue gas cooler is connected to the dust remover, the outlet of the dust remover is connected to the lower section of the cooling tower, the flue gas outlet at the top of the cooling tower is connected to the bottom of the drying tower, the cooling liquid outlet at the lower part of the cooling tower is connected to the cooling liquid inlet of the cooler through the cooling circulating pump, the cooling liquid outlet of the cooler is connected to the cooling liquid inlet of the cold energy recoverer, and the cooling liquid outlet of the cold energy recoverer is connected to the upper part of the cooling tower;
The dry flue gas outlet at the top of the drying tower is connected to the flue gas inlet of the sub-cooler, the flue gas outlet of the sub-cooler is connected to the bottom of the adsorption tower, the outlet at the top of the adsorption tower is connected to the flue gas inlet of the cold energy recoverer, and the flue gas outlet of the cold energy recoverer is connected to a chimney through a No. 2 fan;
The cooling liquid inlet of the cryogenic cooler is connected to the outlet of the cooling unit, and the cooling liquid outlet of the cryogenic cooler is connected with the inlet of the cooling unit;
The high-temperature flue gas cooler air end inlet is connected with the No. 1 fan, the high-temperature flue gas cooler air end outlet is respectively connected to the chimney, the upper end of the drying tower and the upper end of the adsorption tower, the air outlet at the lower end of the drying tower is connected to the atmosphere for evacuation, and the regenerated gas outlet at the lower end of the adsorption tower is connected to the downstream purification recovery section.
Further, the cooling liquid in the cooling tower is water.
Further, a molecular sieve or silica gel is arranged in the drying tower.
Further, the adsorption tower is internally provided with activated carbon.
Further, two drying towers, namely a 1# drying tower and a 2# drying tower, are arranged, and flue gas outlets at the top of the cooling tower are respectively connected to the bottoms of the 1# drying tower and the 2# drying tower; the dry flue gas outlets at the tops of the No. 1 drying tower and the No. 2 drying tower are connected to the flue gas inlet of the cryocooler; one path of the high-temperature flue gas cooler air end outlet connected to the drying tower is connected to the upper ends of the No. 1 drying tower and the No. 2 drying tower respectively, and the air outlets at the lower ends of the No. 1 drying tower and the No. 2 drying tower are connected to the atmosphere for evacuation.
Further, two adsorption towers, namely a 1# adsorption tower and a 2# adsorption tower, are arranged, the flue gas outlets of the cryogenic cooler are respectively connected to the bottoms of the 1# adsorption tower and the 2# adsorption tower, and the outlets at the tops of the 1# adsorption tower and the 2# adsorption tower are both connected to the flue gas inlet of the cold energy recoverer; one path of the high-temperature flue gas cooler air end outlet connected to the adsorption tower is connected to the upper ends of the No. 1 adsorption tower and the No. 2 adsorption tower respectively, and the regenerated gas outlets at the lower ends of the No. 1 adsorption tower and the No. 2 adsorption tower are connected to the downstream purification recovery section.
The method for removing acid gas in flue gas comprises the steps of performing primary heat exchange on high-temperature flue gas of a coal-fired boiler through an air preheater, cooling the flue gas in the high-temperature flue gas cooler again, removing dust through a dust remover, reducing the dust concentration to below 10mg/m 3, cooling the dust-removed flue gas to 5-10 ℃ through a cooling tower, performing heat exchange on cooling liquid in the cooling tower and a cold energy recoverer, recycling, and recycling waste water removed in the flue gas, and delivering the waste water to a waste water treatment system for centralized treatment;
the flue gas at the top of the cooling tower is sent to a drying tower for fine dehydration, the moisture content of the flue gas after fine dehydration is not more than 10ppm, the flue gas after drying by the drying tower is sent to a cryogenic cooler for deep cooling, the temperature is reduced to-20 to-30 ℃, and the cooling capacity is provided by a cooling unit;
The cryogenic low-temperature flue gas is sent to an adsorption tower, SO 2,NOX acid gas in the flue gas is adsorbed once through the adsorption tower, the concentration of SO 2 at the outlet of the adsorption tower and the concentration of NO X are not more than 1mg/m 3, and the low-temperature flue gas purified by the adsorption tower is sent to a chimney for emission after cold energy is recovered by a cold energy recoverer.
Further, two drying towers are connected in parallel, one drying tower is used, the other drying tower is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler, and the two drying towers work alternately.
Further, two adsorption towers are connected in parallel, one adsorption tower is used, the other adsorption tower is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler, a regenerated gas outlet is led to a downstream purification recovery working section, and the two adsorption towers work alternately.
Compared with the prior art, the invention has the following beneficial technical effects:
According to the invention, the acid gas components in the coal-fired flue gas are integrally removed, the flue gas is dehydrated and cooled through the cooling tower, the removed wastewater is intensively recycled, zero emission of wastewater is realized, the high-temperature flue gas cooler is arranged to exchange heat with air, the temperature of the flue gas is reduced, the heat of the high-temperature flue gas is recycled, the drying agent in the drying tower is heated, dehydrated and regenerated through medium-temperature air, the adsorbent in the adsorption tower is heated and regenerated, the heat of the high-temperature flue gas is fully recycled, the cold energy of the low-temperature flue gas discharged from the top of the adsorption tower is recycled through the cold energy recycling device, the cooling liquid is used for cooling again, the adsorption tower is arranged under the low-temperature working condition, the acid gas in the flue gas is adsorbed once, the initial investment is small, the occupied area is saved, and no secondary pollution exists.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention.
Fig. 1 is a schematic structural view of the present invention.
The high-temperature flue gas cooler comprises a high-temperature flue gas cooler 1, a fan 1, a dust remover 3, a cooling tower 4, a cooling circulating pump 5, a cooler 6, a cold energy recoverer 7, a drying tower 1, a drying tower 2, a cooling unit 10, a cryogenic cooler 11, an adsorption tower 1, an adsorption tower 13, and a fan 2.
Detailed Description
The present invention is described in further detail below:
Referring to fig. 1, a system for removing acid gas in flue gas comprises a high-temperature flue gas cooler 1, a # 1 fan 2, a dust remover 3, a cooling tower 4, a cooling circulation pump 5, a cooler 6, a cold energy recoverer 7, a drying tower, a cooling unit 10, a sub-cooler 11, an adsorption tower and a # 2 fan 14;
The flue gas inlet of the high-temperature flue gas cooler 1 is connected to a high-temperature flue gas outlet of the power plant air preheater, the flue gas outlet of the high-temperature flue gas cooler 1 is connected to a dust remover 3, the outlet of the dust remover 3 is connected to the lower section of a cooling tower 4, process water is arranged in the cooling tower 4 as cooling liquid, the flue gas outlet at the top of the cooling tower 4 is connected to the bottom of a drying tower, molecular sieves or silica gel are arranged in the drying tower, the cooling liquid outlet at the lower part of the cooling tower 4 is connected to the cooling liquid inlet of a cooler 6 through a cooling circulation pump 5, the cooling liquid outlet of the cooler 6 is connected to the cooling liquid inlet of a cold energy recoverer 7, and the cooling liquid outlet of the cold energy recoverer 7 is connected to the upper part of the cooling tower 4; the dry flue gas outlet at the top of the drying tower is connected to the flue gas inlet of the sub-cooler 11, the flue gas outlet of the sub-cooler 11 is connected to the bottom of the adsorption tower, activated carbon is arranged in the adsorption tower, the outlet at the top of the adsorption tower is connected to the flue gas inlet of the cold energy recoverer 7, and the flue gas outlet of the cold energy recoverer 7 is connected to a chimney through a 2# fan 14; the cooling liquid inlet of the cryogenic cooler 11 is connected to the outlet of the cooling unit 10, and the cooling liquid outlet of the cryogenic cooler 11 is connected with the inlet of the cooling unit 10; the high-temperature flue gas cooler 1 air end inlet is connected with the No. 1 fan 2, the high-temperature flue gas cooler 1 air end outlet is connected to the upper end of the chimney, the drying tower and the upper end of the adsorption tower respectively, the air outlet at the lower end of the drying tower is connected to the atmosphere evacuation, and the regenerated gas outlet at the lower end of the adsorption tower is connected to the downstream purification recovery section.
The two drying towers are respectively a No. 1 drying tower 8 and a No. 2 drying tower 9, and flue gas outlets at the top of the cooling tower 4 are respectively connected to the bottoms of the No. 1 drying tower 8 and the No. 2 drying tower 9; the dry flue gas outlets at the tops of the No. 1 drying tower 8 and the No. 2 drying tower 9 are connected to the flue gas inlet of the cryocooler 11; one path of the high-temperature flue gas cooler 1 air end outlet connected to the drying tower is connected to the upper ends of the No. 1 drying tower 8 and the No. 2 drying tower 9 respectively, and the air outlets at the lower ends of the No. 1 drying tower 8 and the No. 2 drying tower 9 are connected to the atmosphere for evacuation.
The two adsorption towers are respectively a 1# adsorption tower 12 and a 2# adsorption tower 13, the flue gas outlets of the cryocooler 11 are respectively connected to the bottoms of the 1# adsorption tower 12 and the 2# adsorption tower 13, and the outlets at the tops of the 1# adsorption tower 12 and the 2# adsorption tower 13 are both connected to the flue gas inlet of the cold energy recoverer 7; one path of the high-temperature flue gas cooler 1, which is connected to the air end outlet of the adsorption tower, is respectively connected to the upper ends of the No. 1 adsorption tower 12 and the No. 2 adsorption tower 13, and the regenerated gas outlets at the lower ends of the No. 1 adsorption tower 12 and the No. 2 adsorption tower 13 are connected to the downstream purification recovery section.
In order to clearly illustrate the present invention, the present invention will be described in further detail with reference to the following examples and the accompanying drawings. It will be appreciated by persons skilled in the art that the following is not intended to limit the scope of the invention, and that any modifications and variations made on the basis of the present invention are within the scope of the invention.
Referring to fig. 1, an acid gas removal system in flue gas comprises a high-temperature flue gas cooler 1 connected with a high-temperature flue gas outlet of an air preheater of a power plant, wherein the flue gas outlet of the high-temperature flue gas cooler 1 is connected with a dust remover 3, the flue gas after dust removal is connected with the lower section of a cooling tower 4, process water is arranged in the cooling tower 4 as cooling liquid, the flue gas after washing and cooling by the cooling tower 4 goes to the bottom of a No. 1 drying tower 8 or the bottom of a No. 2 drying tower 9 from the top of the cooling tower 4, the cooling liquid at the bottom of the cooling tower 4 goes to an inlet of a cooling circulation pump 5, the cooling circulation pump 5 is connected with a cooling liquid inlet end of a cooler 6, a cooling liquid outlet end of the cooler 6 is connected with a cooling liquid inlet end of a cooling liquid recovery 7, and a cooling liquid outlet end of the cooling liquid recovery 7 is communicated with the upper end of the cooling tower 4.
The dry flue gas dried by the No. 1 drying tower 8 and the No. 2 drying tower 9 is sent to the cryocooler 11, the flue gas outlet of the cryocooler 11 is connected with the bottoms of the No. 1 adsorption tower 12 and the No. 2 adsorption tower 13, the purified low-temperature flue gas is sent to the flue gas inlet of the cold energy recoverer 7, the flue gas outlet of the cold energy recoverer 7 is connected with the inlet of the No. 2 fan 14, and the outlet of the No. 2 fan 14 is sent to a chimney.
Molecular sieves or silica gel are arranged in the No.1 drying tower 8 and the No. 2 drying tower 9.
The No. 1 adsorption tower 12 and the No. 2 adsorption tower 13 are internally provided with carefully selected activated carbon.
The cooling liquid inlet end of the cryocooler 11 is connected with the outlet of the cooling unit 10, and the cooling liquid outlet end of the cryocooler 11 is connected with the inlet of the cooling unit 10.
The inlet of the air end of the high-temperature flue gas cooler 1 is connected with the outlet of the 1# fan 2, the 1# fan 2 is communicated with the air, the outlet of the air end of the high-temperature flue gas cooler 1 is divided into three paths, one path of the air is sent to a chimney, the other path of the air is sent to the upper end of the 1# drying tower 8 or the upper end of the 2# drying tower 9, the other path of the air is sent to the upper end of the 1# adsorption tower 12 and the upper end of the 2# adsorption tower 13, the air outlets of the lower ends of the 1# drying tower 8 and the 2# drying tower 9 are sent to the atmosphere for evacuation, and the regenerated gas outlets of the lower ends of the 1# adsorption tower 12 and the 2# adsorption tower 13 are sent to a downstream purification recovery section.
The technological process and principle of the invention are as follows:
the high-temperature flue gas of the coal-fired boiler is subjected to primary heat exchange through an air preheater, enters a high-temperature flue gas cooler 1 for cooling again, is subjected to dust removal through a dust remover 3, reduces the dust concentration to below 10mg/m 3, the flue gas after dust removal is subjected to water washing and cooling to 5-10 ℃ through a cooling tower 4, water washing liquid in the cooling tower 4 is subjected to heat exchange with a cold energy recoverer through a cooler 6 and then is recycled, and wastewater removed from the flue gas is recovered and sent to a wastewater treatment system for centralized treatment.
The flue gas at the top of the cooling tower 4 is sent to a drying tower for fine dehydration, a molecular sieve or silica gel is arranged in the drying tower, the moisture content of the flue gas after fine dehydration is not more than 10ppm, two drying towers are connected in parallel, one drying tower is used, the other drying tower is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler 1, and the two drying towers alternately work.
The flue gas dried by the drying tower is sent to a cryogenic cooler 11 for deep cooling, the temperature is reduced to minus 20 to minus 30 ℃, and the cooling capacity is provided by a cooling unit 10.
The cryogenic low-temperature flue gas is sent to an adsorption tower, carefully chosen active carbon is arranged in the adsorption tower, acid gases such as SO 2,NOX and the like in the flue gas are adsorbed at one time, the concentration of SO 2 at the outlet of the adsorption tower and the concentration of NO X are not more than 1mg/m 3, two adsorption towers are connected in parallel, one adsorption tower is used, the other adsorption tower is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler 1, the regenerated gas outlet is sent to a downstream purification and recovery working section, and the two adsorption towers work alternately.
The low-temperature flue gas purified by the adsorption tower is sent to a chimney for emission after cold energy is recovered by the cold energy recoverer 7.
Claims (4)
1. The system for removing the acid gas in the flue gas is characterized by comprising a high-temperature flue gas cooler (1), a No. 1 fan (2), a dust remover (3), a cooling tower (4), a cooling circulating pump (5), a cooler (6), a cold energy recoverer (7), a drying tower, a cooling unit (10), a cryogenic cooler (11), an adsorption tower and a No. 2 fan (14);
The flue gas inlet of the high-temperature flue gas cooler (1) is connected to the high-temperature flue gas outlet of the air preheater of the power plant, the flue gas outlet of the high-temperature flue gas cooler (1) is connected to the dust remover (3), the outlet of the dust remover (3) is connected to the lower section of the cooling tower (4), the flue gas outlet at the top of the cooling tower (4) is connected to the bottom of the drying tower, the cooling liquid outlet at the lower part of the cooling tower (4) is connected to the cooling liquid inlet of the cooler (6) through the cooling circulating pump (5), the cooling liquid outlet of the cooler (6) is connected to the cooling liquid inlet of the cold energy recoverer (7), and the cooling liquid outlet of the cold energy recoverer (7) is connected to the upper part of the cooling tower (4);
The dry flue gas outlet at the top of the drying tower is connected to the flue gas inlet of the cryogenic cooler (11), the flue gas outlet of the cryogenic cooler (11) is connected to the bottom of the adsorption tower, the outlet at the top of the adsorption tower is connected to the flue gas inlet of the cold energy recoverer (7), and the flue gas outlet of the cold energy recoverer (7) is connected to a chimney through a No. 2 fan (14);
The cooling liquid inlet of the cryogenic cooler (11) is connected to the outlet of the cooling unit (10), and the cooling liquid outlet of the cryogenic cooler (11) is connected with the inlet of the cooling unit (10);
The high-temperature flue gas cooler (1) air end inlet is connected with the No.1 fan (2), the high-temperature flue gas cooler (1) air end outlet is respectively connected to a chimney, the upper end of a drying tower and the upper end of an adsorption tower, the air outlet at the lower end of the drying tower is connected to the atmosphere for evacuation, and the regenerated gas outlet at the lower end of the adsorption tower is connected to the downstream purification and recovery section;
The two drying towers are respectively a 1# drying tower (8) and a 2# drying tower (9), and flue gas outlets at the top of the cooling tower (4) are respectively connected to the bottoms of the 1# drying tower (8) and the 2# drying tower (9); the dry flue gas outlets at the tops of the No. 1 drying tower (8) and the No. 2 drying tower (9) are connected to the flue gas inlet of the cryocooler (11); one path of the air outlet of the high-temperature flue gas cooler (1) is connected to the upper ends of the No. 1 drying tower (8) and the No. 2 drying tower (9), and the air outlets of the lower ends of the No. 1 drying tower (8) and the No. 2 drying tower (9) are connected to the atmosphere for evacuation;
The two adsorption towers are respectively a 1# adsorption tower (12) and a 2# adsorption tower (13), the flue gas outlets of the cryogenic cooler (11) are respectively connected to the bottoms of the 1# adsorption tower (12) and the 2# adsorption tower (13), and the outlets at the tops of the 1# adsorption tower (12) and the 2# adsorption tower (13) are both connected to the flue gas inlet of the cold energy recoverer (7); one path of the air end outlet of the high-temperature flue gas cooler (1) is connected to the adsorption tower, one path of the air end outlet of the high-temperature flue gas cooler is connected to the upper ends of the No.1 adsorption tower (12) and the No. 2 adsorption tower (13), and the regenerated gas outlets at the lower ends of the No.1 adsorption tower (12) and the No. 2 adsorption tower (13) are connected to the downstream purification and recovery working section; the cooling liquid in the cooling tower (4) is water; a molecular sieve or silica gel is arranged in the drying tower; and activated carbon is arranged in the adsorption tower.
2. The method for removing acid gas in flue gas is characterized in that high-temperature flue gas of a coal-fired boiler is subjected to primary heat exchange through an air preheater, enters a high-temperature flue gas cooler (1) for cooling again, is subjected to dust removal through a dust remover (3), the dust concentration is reduced to be below 10mg/m 3, the flue gas after dust removal is cooled to 5-10 ℃ through a cooling tower (4), cooling liquid in the cooling tower (4) is subjected to heat exchange with a cold energy recoverer (7) and then is recycled, and waste water removed in the flue gas is recovered and sent to a waste water treatment system for centralized treatment;
The flue gas at the top of the cooling tower (4) is sent to a drying tower for fine dehydration, the moisture content of the flue gas after fine dehydration is not more than 10ppm, the flue gas after drying by the drying tower is sent to a cryogenic cooler (11) for deep cooling, the temperature is reduced to-20 to-30 ℃, and the cooling capacity is provided by a cooling unit (10);
The cryogenic low-temperature flue gas is sent to an adsorption tower, SO 2,NOX acid gas in the flue gas is adsorbed once through the adsorption tower, the concentration of SO 2 at the outlet of the adsorption tower and the concentration of NO X are not more than 1mg/m 3, and the cryogenic flue gas purified by the adsorption tower is sent to a chimney for emission after cold energy is recovered by a cold energy recoverer (7).
3. The method for removing acid gases from flue gas according to claim 2, wherein two drying towers are arranged in parallel, one is used, the other is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler (1), and the two drying towers work alternately.
4. The method for removing acid gases from flue gas according to claim 2, wherein two adsorption towers are arranged in parallel, one adsorption tower is used, the other adsorption tower is heated and regenerated by hot air exchanging heat with the high-temperature flue gas cooler (1), a regenerated gas outlet is led to a downstream purification and recovery section, and the two adsorption towers work alternately.
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