CN111841066A - 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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- CN111841066A CN111841066A CN202010820823.4A CN202010820823A CN111841066A CN 111841066 A CN111841066 A CN 111841066A CN 202010820823 A CN202010820823 A CN 202010820823A CN 111841066 A CN111841066 A CN 111841066A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 147
- 239000003546 flue gas Substances 0.000 title claims abstract description 147
- 239000007789 gas Substances 0.000 title claims abstract description 41
- 239000002253 acid Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000001179 sorption measurement Methods 0.000 claims abstract description 96
- 238000001035 drying Methods 0.000 claims abstract description 90
- 238000001816 cooling Methods 0.000 claims abstract description 72
- 239000000110 cooling liquid Substances 0.000 claims abstract description 24
- 239000002351 wastewater Substances 0.000 claims abstract description 7
- 239000000428 dust Substances 0.000 claims description 19
- 238000011084 recovery Methods 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 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
- 238000004064 recycling Methods 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims description 3
- 239000003463 adsorbent Substances 0.000 abstract description 2
- 239000002274 desiccant Substances 0.000 abstract description 2
- 239000002826 coolant Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 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
- 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
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 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
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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)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- 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, wherein acid gas components in coal-fired flue gas are removed integrally, the flue gas is dehydrated and cooled by arranging a cooling tower, the removed waste water is recovered and treated in a centralized manner, zero emission of waste water is realized, the temperature of the flue gas is reduced by arranging a high-temperature flue gas cooler to exchange heat with air, simultaneously, the heat of high-temperature flue gas is recovered, a drying agent in a drying tower is heated, dehydrated and regenerated by using medium-temperature air, an adsorbent in an adsorption tower is heated and regenerated, the heat of the high-temperature flue gas is fully recycled, the cold quantity of low-temperature flue gas discharged from the top of the adsorption tower is recovered by arranging a cold quantity recoverer and is used for cooling liquid again, the adsorption tower is arranged under the low-temperature working condition, the acid gas in the flue gas is adsorbed once, the.
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 acidic waste gas pollutants, such as smoke dust and SO2NOx and the like seriously affect the balance of ecological environment and the physical health of people. NOx is mainly composed of NO and also contains a small amount of NO2. At present, the mainstream flue gas purification technology is to perform desulfurization, denitrification and dust removal by adopting the combination of SCR denitration, ESP electric precipitation and FGD wet desulphurization.
The traditional flue gas desulfurization and denitration adopt a separate treatment method, although a certain achievement is achieved, the equipment is huge, the technology is complex, the cost is overhigh, and great influence is caused to the development of a thermal power plant. For example, the FGD wet desulphurization technology occupies a large area, needs a large amount of limestone as an auxiliary absorbent, is easy to corrode and scale the inner wall of the equipment and has high maintenance difficulty. The SCR denitration technology has high initial investment cost, ammonia or urea needs to be continuously consumed as a reducing agent, and the SCR catalyst is easy to be poisoned and invalid, has high treatment difficulty and high operation cost. Therefore, the research of novel and efficient flue gas desulfurization and denitration technology becomes the focus of the 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, can simultaneously remove the acid gas in coal-fired flue gas, and has the advantages of high removal efficiency, low operation cost and easy maintenance of a device.
In order to achieve the purpose, the invention adopts the following technical scheme:
a system for removing acid gas in 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 energy recoverer, a drying tower, a refrigerating unit, a cryogenic cooler, an adsorption tower and a No. 2 fan;
the cooling tower comprises a high-temperature flue gas cooler, a dust remover, a cooling tower, a drying tower, a cooling circulation pump, a cooling capacity recoverer, a cooling capacity recovery device and a cooling capacity recovery device, wherein a flue gas inlet of the high-temperature flue gas cooler is connected to a high-temperature flue gas outlet of an air preheater of a power plant, a flue gas outlet of the high-temperature flue gas cooler is connected to the dust remover, an outlet of the dust remover is connected to the lower section of the cooling tower, a flue gas outlet at the top of the cooling tower is connected to the bottom of the drying tower, a cooling liquid outlet at the lower part;
a dry flue gas outlet at the top of the drying tower is connected to a flue gas inlet of a cryogenic cooler, a flue gas outlet of the cryogenic cooler is connected to the bottom of the adsorption tower, an outlet at the top of the adsorption tower is connected to a flue gas inlet of a cold energy recoverer, and a flue gas outlet of the cold energy recoverer is connected to a chimney through a No. 2 fan;
a cooling liquid inlet of the cryogenic cooler is connected with an outlet of the cooling unit, and a cooling liquid outlet of the cryogenic cooler is connected with an inlet of the cooling unit;
the inlet of the air end of the high-temperature flue gas cooler is connected with a No. 1 fan, the outlet of the air end of the high-temperature flue gas cooler is respectively connected to the upper ends of a chimney, a drying tower and an adsorption tower, the air outlet at the lower end of the drying tower is connected to atmosphere evacuation, and the regenerated gas outlet at the lower end of the adsorption tower is connected to a downstream purification and 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, active carbon is arranged in the adsorption tower.
Furthermore, the drying towers are two, namely a No. 1 drying tower and a No. 2 drying tower, and the flue gas outlets at the top of the cooling tower are respectively connected to the bottoms of the No. 1 drying tower and the No. 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 a flue gas inlet of a cryogenic cooler; the outlet of the air end of the high-temperature flue gas cooler is connected to one path of the drying tower and is respectively connected to the upper ends of the 1# drying tower and the 2# drying tower, and the outlet of the air at the lower ends of the 1# drying tower and the 2# drying tower is connected to the atmosphere for emptying.
Furthermore, the adsorption towers are two, namely a 1# adsorption tower and a 2# adsorption tower, a flue gas outlet of the cryogenic cooler is connected to the bottoms of the 1# adsorption tower and the 2# adsorption tower respectively, and outlets at the tops of the 1# adsorption tower and the 2# adsorption tower are connected to a flue gas inlet of the cold energy recoverer; the outlet of the air end of the high-temperature flue gas cooler is connected to one path of the adsorption tower and is respectively connected to the upper ends of the 1# adsorption tower and the 2# adsorption tower, and the outlet of the regenerated gas at the lower ends of the 1# adsorption tower and the 2# adsorption tower is connected to the downstream purification and recovery section.
A method for removing acidic gas from fume includes such steps as primary heat exchange of high-temp fume in air preheater, cooling in high-temp fume cooler, and removing dust by duster to reduce dust concentration to 10mg/m3Cooling the dedusted flue gas to 5-10 ℃ through a cooling tower, carrying out heat exchange on cooling liquid in the cooling tower and a cold energy recoverer through a cooler, recycling, and recycling the wastewater removed from the flue gas to a wastewater 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 deep cooling cooler for deep cooling, the temperature is reduced to-20 to-30 ℃, and the cooling capacity is provided by a cooling unit;
sending the cryogenic low-temperature flue gas to an adsorption tower, and passing SO in the flue gas through the adsorption tower2，NOXOne-time adsorption of acid gas, adsorption tower outlet SO2Concentration and NOXThe concentration is not more than 1mg/m3And the low-temperature flue gas purified by the adsorption tower is discharged to a chimney after the cold energy is recovered by a cold energy recoverer.
Furthermore, 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.
Furthermore, the 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 communicated to a downstream purification and recovery working section, and the two adsorption towers work alternately.
Compared with the prior art, the invention has the following beneficial technical effects:
the invention integrally removes acid gas components in coal-fired flue gas, dehydrates and cools the flue gas by arranging the cooling tower, intensively recovers and treats the removed wastewater, realizes zero discharge of the wastewater, reduces the temperature of the flue gas by arranging the high-temperature flue gas cooler to exchange heat with air, recovers the heat of the high-temperature flue gas, heats and dehydrates a drying agent in a drying tower by using medium-temperature air, heats and regenerates an adsorbent in an adsorption tower, fully recycles the heat of the high-temperature flue gas, recovers the cold of low-temperature flue gas discharged from the top of the adsorption tower by arranging the cold energy recoverer, is used for cooling a cooling liquid again, arranges the adsorption tower under the low-temperature working condition, adsorbs the acid gas in the flue gas once, has small initial investment, saves occupied land and does not have secondary pollution.
Drawings
The accompanying drawings 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 and not to limit the invention.
FIG. 1 is a schematic structural diagram of the present invention.
The system comprises a high-temperature flue gas cooler 1, a fan 1# 2, a dust remover 3, a cooling tower 4, a cooling circulating pump 5, a cooler 6, a cold recovery device 7, a drying tower 1# 8, a drying tower 2# 9, a refrigerating unit 10, a cryogenic cooler 11, an adsorption tower 1# 12, an adsorption tower 2# 13 and a fan 2# 14.
Detailed Description
The 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 circulating pump 5, a cooler 6, a cold energy recoverer 7, a drying tower, a refrigerating unit 10, a cryogenic cooler 11, an adsorption tower and a # 2 fan 14;
a flue gas inlet of the high-temperature flue gas cooler 1 is connected to a high-temperature flue gas outlet of an air preheater of a power plant, a flue gas outlet of the high-temperature flue gas cooler 1 is connected to a dust remover 3, an 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 to serve as cooling liquid, a flue gas outlet at the top of the cooling tower 4 is connected to the bottom of a drying tower, a molecular sieve or silica gel is arranged in the drying tower, a cooling liquid outlet at the lower part of the cooling tower 4 is connected to a cooling liquid inlet of a cooler 6 through a cooling circulating pump 5, a cooling liquid outlet of the cooler 6 is connected to a cooling liquid inlet of a cooling capacity recoverer 7; a dry flue gas outlet at the top of the drying tower is connected to a flue gas inlet of a cryogenic cooler 11, a flue gas outlet of the cryogenic cooler 11 is connected to the bottom of an adsorption tower, activated carbon is arranged in the adsorption tower, an outlet at the top of the adsorption tower is connected to a flue gas inlet of a cold energy recoverer 7, and a flue gas outlet of the cold energy recoverer 7 is connected to a chimney through a No. 2 fan 14; a cooling liquid inlet of the cryogenic cooler 11 is connected with an outlet of the cooling unit 10, and a cooling liquid outlet of the cryogenic cooler 11 is connected with an inlet of the cooling unit 10; an inlet of an air end of the high-temperature flue gas cooler 1 is connected with the No. 1 fan 2, an outlet of the air end of the high-temperature flue gas cooler 1 is connected to the upper ends of a chimney and a drying tower and the upper end of an adsorption tower respectively, an air outlet at the lower end of the drying tower is connected to atmosphere evacuation, and a regenerated gas outlet at the lower end of the adsorption tower is connected to a downstream purification and recovery section.
The two drying towers are respectively a No. 1 drying tower 8 and a No. 2 drying tower 9, and the 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 cryogenic cooler 11; the outlet of the air end of the high-temperature flue gas cooler 1 is connected to one path of the drying tower and is respectively connected to the upper ends of the No. 1 drying tower 8 and the No. 2 drying tower 9, and the air outlet of the lower ends of the No. 1 drying tower 8 and the No. 2 drying tower 9 is connected to the atmosphere for emptying.
The adsorption towers are two, namely a 1# adsorption tower 12 and a 2# adsorption tower 13, a flue gas outlet of the cryogenic cooler 11 is connected to the bottoms of the 1# adsorption tower 12 and the 2# adsorption tower 13 respectively, and outlets at the tops of the 1# adsorption tower 12 and the 2# adsorption tower 13 are connected to a flue gas inlet of the cold energy recoverer 7; an outlet of an air end of the high-temperature flue gas cooler 1 is connected to one path of the adsorption tower and is respectively connected to the upper ends of the adsorption tower No. 1 12 and the adsorption tower No. 2 13, and a regenerated gas outlet at the lower ends of the adsorption tower No. 1 and the adsorption tower No. 2 13 is connected to a downstream purification and recovery section.
For the purpose of clarity, the present invention will be described in further detail with reference to the following examples and accompanying drawings. It will be understood by those skilled in the art that the following descriptions are not intended to limit the scope of the present invention, and that any modifications or variations based on the present invention are within the scope of the present invention.
Referring to fig. 1, an acid gas desorption system in flue gas, include the high temperature flue gas cooler 1 that links to each other with the air preheater high temperature exhanst gas outlet of power plant, the exhanst gas outlet of high temperature flue gas cooler 1 links to each other with dust remover 3, the flue gas after the dust removal links to each other with cooling tower 4 hypomere, be equipped with the process water as the coolant liquid in the cooling tower 4, the flue gas after 4 washing cooling of cooling tower is gone to 1# drying tower 8 bottom or 2# drying tower 9 bottom from cooling tower 4 top, the coolant liquid of cooling tower 4 bottom goes to cooling circulation pump 5 entry, cooling circulation pump 5 links to each other with 6 coolant liquid entry end of cooler, 6 coolant liquid exit end of cooler links to each other with 7 coolant liquid entry ends of cold volume recoverer, 7 coolant liquid exit ends of cold volume communicate with cooling tower.
Dry flue gas after 8 and 9 # drying towers of 1# drying tower is to cryogenic cooler 11, and 11 exhanst gas outlets of cryogenic cooler link to each other with 12 bottoms of 1# adsorption tower and 13 bottoms of 2# adsorption tower, and the low temperature flue gas after the purification is to 7 flue gas inlets of cold volume recoverer, and 7 exhanst gas outlets of cold volume recoverer link to each other with 14 entrances of 2# fan, and the chimney is to in 14 exports of 2# fan.
Molecular sieves or silica gel are arranged in the No. 1 drying tower 8 and the No. 2 drying tower 9.
The # 1 adsorption tower 12 and the # 2 adsorption tower 13 are internally provided with concentrated activated carbon.
11 coolant inlet ends of cryocoolers are connected with the outlet of refrigerating unit 10, and 11 coolant outlet ends of cryocoolers are connected with the inlet of refrigerating unit 10.
The inlet of the air end of the high-temperature flue gas cooler 1 is connected with the outlet of the fan 1# 2, the fan 1# 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 goes to a chimney, the other path goes to the upper end of the drying tower 1# 8 or the upper end of the drying tower 2# 9, the other path goes to the upper end of the adsorption tower 1# 12 and the upper end of the adsorption tower 2# 13, the air outlets at the lower ends of the drying tower 1# 8 and the drying tower 2# 9 go to the atmosphere for emptying, and the regenerated gas outlet at the lower ends of the adsorption tower 1# 12 and.
The process and the principle of the invention are as follows:
the high-temperature flue gas of the coal-fired boiler is subjected to primary heat exchange by an air preheater, enters the high-temperature flue gas cooler 1 for secondary cooling, is dedusted by the deduster 3 to reduce the dust concentration to 10mg/m3And then, washing the dedusted flue gas by a cooling tower 4 to reduce the temperature to 5-10 ℃, exchanging heat between a washing liquid in the cooling tower 4 and a cold energy recoverer through a cooler 6 and then recycling, and recovering the wastewater removed from the flue gas to a wastewater treatment system for centralized treatment.
Flue gas at the top of the cooling tower 4 goes 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, the 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 work alternately.
The flue gas dried by the drying tower goes to a deep cooling cooler 11 for deep cooling, the temperature is reduced to-20 to-30 ℃, and the cold energy is provided by a refrigerating unit 10.
The cryogenic low-temperature flue gas goes to an adsorption tower, fine-selected active carbon is arranged in the adsorption tower, and SO in the flue gas is removed2，NOXWhen the acid gas is adsorbed at one time, the SO at the outlet of the adsorption tower2Concentration and NOXThe concentration is not more than 1mg/m3The 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, and regenerated gas is dischargedThe port is communicated with 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 discharged to a chimney after the cold energy is recovered by a cold energy recoverer 7.
Claims (9)
1. A system for removing acid gas in 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 refrigerating 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 an air preheater of a 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 a 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;
a dry flue gas outlet at the top of the drying tower is connected to a flue gas inlet of a cryogenic cooler (11), a flue gas outlet of the cryogenic cooler (11) is connected to the bottom of the adsorption tower, an outlet at the top of the adsorption tower is connected to a flue gas inlet of a cold energy recoverer (7), and a flue gas outlet of the cold energy recoverer (7) is connected to a chimney through a No. 2 fan (14);
a cooling liquid inlet of the cryogenic cooler (11) is connected to an outlet of the cooling unit (10), and a cooling liquid outlet of the cryogenic cooler (11) is connected with an inlet of the cooling unit (10);
the air end inlet of the high-temperature flue gas cooler (1) is connected with the No. 1 fan (2), the air end outlet of the high-temperature flue gas cooler (1) is respectively connected to the upper ends of a chimney and 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 atmosphere evacuation, and the regenerated gas outlet at the lower end of the adsorption tower is connected to a downstream purification recovery section.
2. The system for removing the acid gases in the flue gas according to claim 1, wherein the cooling liquid in the cooling tower (4) is water.
3. The system for removing acid gases in flue gas according to claim 1, wherein a molecular sieve or silica gel is arranged in the drying tower.
4. The system for removing acid gases in flue gas according to claim 1, wherein activated carbon is arranged in the adsorption tower.
5. The system for removing the acid gas in the flue gas according to claim 1, wherein the number of the drying towers is two, namely a # 1 drying tower (8) and a # 2 drying tower (9), and the flue gas outlet at the top of the cooling tower (4) is connected to the bottoms of the # 1 drying tower (8) and the # 2 drying tower (9), respectively; 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 a flue gas inlet of a cryogenic cooler (11); the outlet of the air end of the high-temperature flue gas cooler (1) is connected to one path of the drying tower and is respectively connected to the upper ends of the 1# drying tower (8) and the 2# drying tower (9), and the air outlets at the lower ends of the 1# drying tower (8) and the 2# drying tower (9) are connected to the atmosphere for emptying.
6. The system for removing the acid gas in the flue gas according to claim 1, wherein the adsorption towers are provided with two adsorption towers, namely a # 1 adsorption tower (12) and a # 2 adsorption tower (13), the flue gas outlet of the cryogenic cooler (11) is 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 connected to the flue gas inlet of the cold energy recoverer (7); an outlet of an air end of the high-temperature flue gas cooler (1) is connected to one path of the adsorption tower and is respectively connected to the upper ends of a 1# adsorption tower (12) and a 2# adsorption tower (13), and a regenerated gas outlet at the lower ends of the 1# adsorption tower (12) and the 2# adsorption tower (13) is connected to a downstream purification and recovery section.
7. A method for removing acid gas in flue gas, which comprises the step of using the acid in flue gas as claimed in claim 1The system for removing the sex gas is characterized in that high-temperature flue gas of a coal-fired boiler is subjected to primary heat exchange by an air preheater, enters a high-temperature flue gas cooler (1) for secondary cooling, is dedusted by a deduster (3), and is used for reducing the dust concentration to 10mg/m3Cooling the dedusted flue gas to 5-10 ℃ through a cooling tower (4), carrying out heat exchange between cooling liquid in the cooling tower (4) and a cold energy recoverer (7) through a cooler (6) and then recycling the cooling liquid, and recycling the wastewater removed from the flue gas 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, 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);
sending the cryogenic low-temperature flue gas to an adsorption tower, and passing SO in the flue gas through the adsorption tower2，NOXOne-time adsorption of acid gas, adsorption tower outlet SO2Concentration and NOXThe concentration is not more than 1mg/m3And the low-temperature flue gas purified by the adsorption tower is subjected to cold recovery by a cold recovery device (7) and then is discharged to a chimney.
8. The method for removing the acid gases in the flue gas according to claim 7, wherein two drying towers are arranged 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 work alternately.
9. The method for removing the acid gases in the flue gas according to claim 7, 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 sent to a downstream purification and recovery section, and the two adsorption towers work alternately.
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