CN111359408A - Desulfurization and denitrification flue gas comprehensive treatment device and method cooperating with thermal power generation - Google Patents
Desulfurization and denitrification flue gas comprehensive treatment device and method cooperating with thermal power generation Download PDFInfo
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- CN111359408A CN111359408A CN202010367226.0A CN202010367226A CN111359408A CN 111359408 A CN111359408 A CN 111359408A CN 202010367226 A CN202010367226 A CN 202010367226A CN 111359408 A CN111359408 A CN 111359408A
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- flue gas
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- desulfurization
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- fly ash
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- 239000003546 flue gas Substances 0.000 title claims abstract description 125
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 38
- 230000023556 desulfurization Effects 0.000 title claims abstract description 38
- 238000010248 power generation Methods 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000003054 catalyst Substances 0.000 claims abstract description 93
- 239000010881 fly ash Substances 0.000 claims abstract description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 230000003197 catalytic effect Effects 0.000 claims abstract description 30
- 230000000694 effects Effects 0.000 claims abstract description 29
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 20
- 239000000463 material Substances 0.000 claims abstract description 18
- 238000010521 absorption reaction Methods 0.000 claims abstract description 17
- 230000006698 induction Effects 0.000 claims abstract description 16
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 12
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 239000007800 oxidant agent Substances 0.000 claims description 54
- 230000001590 oxidative effect Effects 0.000 claims description 54
- 239000000428 dust Substances 0.000 claims description 27
- 238000005485 electric heating Methods 0.000 claims description 14
- 239000003344 environmental pollutant Substances 0.000 claims description 13
- 231100000719 pollutant Toxicity 0.000 claims description 13
- 238000002347 injection Methods 0.000 claims description 12
- 239000007924 injection Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 12
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 10
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 10
- 238000001514 detection method Methods 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 5
- 238000005260 corrosion Methods 0.000 claims description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 4
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 3
- 239000011248 coating agent Substances 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- 230000007797 corrosion Effects 0.000 claims description 3
- 239000010908 plant waste Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 229910002665 PbTe Inorganic materials 0.000 claims description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910044991 metal oxide Inorganic materials 0.000 claims description 2
- 150000004706 metal oxides Chemical class 0.000 claims description 2
- 239000012286 potassium permanganate Substances 0.000 claims description 2
- OCGWQDWYSQAFTO-UHFFFAOYSA-N tellanylidenelead Chemical compound [Pb]=[Te] OCGWQDWYSQAFTO-UHFFFAOYSA-N 0.000 claims description 2
- 239000010936 titanium Substances 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims 5
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 238000004140 cleaning Methods 0.000 claims 1
- 150000002696 manganese Chemical class 0.000 claims 1
- 238000012544 monitoring process Methods 0.000 claims 1
- 238000003786 synthesis reaction Methods 0.000 claims 1
- 238000007599 discharging Methods 0.000 abstract 1
- 230000005611 electricity Effects 0.000 abstract 1
- 238000003303 reheating Methods 0.000 abstract 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 2
- 239000000306 component Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical group [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000008358 core component Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000002699 waste material 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- 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
- B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/106—Peroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/20707—Titanium
-
- 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
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
Abstract
The invention discloses a desulfurization and denitrification flue gas comprehensive treatment device and method for cooperative thermal power generationXAnd SOXThen enters a deep catalytic unit for deep oxidation, and then enters an absorption tower for removing NOXAnd SOXDemisting, and discharging the flue gas after reheating; thermoelectric induction materials are laid on the wall surface of the hearth to generate electricity, so that power is provided for the whole system; the catalyst is selected to be arranged in multiple stages, the primary catalyst is made of fly ash, the fly ash is sprayed into flue gas after being pretreated to carry out catalytic reaction, the catalyst in the deep catalytic unit is made of high-efficiency desulfurization and denitration catalyst and coated on the surface of a heat exchanger, the temperature of water at an inlet is adjusted by thermal power generation, and then the surface temperature of the heat exchanger is controlled to ensure that the deep catalytic unit is in the optimal reaction condition. An automatic control system is arranged to monitor the average activity and the high activity ratio of the primary catalyst in real time, so that the high efficiency and the economy of the system are ensured.
Description
Technical Field
The invention belongs to the technical field of nitrogen and sulfur oxide environmental pollution treatment, and particularly relates to a desulfurization and denitrification flue gas comprehensive treatment device and method for cooperative thermal power generation.
Background
The phenomenon of atmospheric pollution is a great problem of harming the living environment of human beings, and SO discharged by coal-fired power plants2、NOXThe harm to human health and ecological environment is obvious; wherein, SO2Is the main reason for acid rain, and NOx can generate photochemical smog, destroy the ozone layer and generate greenhouse effect. At present, the most mature methods for removing the two pollutants are wet desulfurization and SCR denitration respectively. However, when the method is used for treating the pollutants in the power plant, serious catalyst waste exists, for example, when a power station boiler is in variable load operation, the content of the pollutant components in the flue gas is greatly changed, and the catalyst is used as a core component for removing the pollutants, for NO and SO2The content of water vapor is sensitive, and when the concentration of the pollutants is changed, the catalytic efficiency of the catalyst is reduced to different degrees. Therefore, to economically and efficiently remove the flue gas pollutants from coal-fired power plants by using the catalyst, the flue gas treatment system of the power plants must be closely combined with the characteristics of the catalyst. In the existing power station flue gas treatment system, pollutants are removed by adopting a single catalyst, and the relationship between the activity of the catalyst and the change of the load of the power station so as to cause the change of flue gas components is not fully considered. Although the traditional flue gas pollutant removal technology has higher removal efficiency, under the situation of intensive economic rapid development, the research of an optimization method capable of realizing the catalyst under the condition of efficiently removing the flue gas pollutants of the power plant is extremely important.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention aims to provide a device and a method for comprehensively treating desulfurization and denitrification flue gas by cooperating with thermal power generation, which can be used for treating NO in the flue gasx、SO2Deep oxidation and removal are carried out, and ultra-clean discharge is realized.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a desulfurization and denitrification flue gas comprehensive treatment device for cooperative thermal power generation comprises a boiler 1, wherein a flue gas cooler 2 is arranged in a flue at the tail part of the boiler 1, a pump I12-2 is arranged at the inlet of the flue gas cooler, an oxidant nozzle and a primary catalyst nozzle are arranged in a flue where the flue gas cooler 2 is connected with a dust remover 4, an oxidant storage tank 3 is connected with the oxidant nozzle through a pipeline, an oxidant power device 12-3 is arranged on the pipeline, a deep catalysis unit 5 is arranged in the flue between the dust remover 4 and an absorption tower 6, and a pump II 12-4 and an electric heating device 16 are arranged at the water side inlet of the deep catalysis unit 5; a demister 7 is arranged at the outlet of the absorption tower 6, and a flue between the demister 7 and a chimney 10 is sequentially provided with a flue gas reheater 8, a draught fan 9 and a recirculated flue gas opening B; the recycling flue gas opening B is connected with a primary catalyst nozzle through a flue gas pipeline, a fan 12-1 is arranged on the flue gas pipeline, a fly ash outlet of the dust remover 4 is divided into two paths, one path is communicated with the primary catalyst nozzle through a pipeline, a catalyst pretreatment device 15 is arranged on the pipeline, and the other path is communicated with a fly ash storage tank 13 through a pipeline; in addition, a thermoelectric induction material is laid on the wall surface of a hearth of the boiler 1, the thermoelectric induction material is connected with an electric storage device 11, the electric storage device 11 and an automatic control system 14 are connected with a fan 12-1, a pump I12-2, an oxidant power device 12-3, a pump II 12-4, an electric heating device 16 and a catalyst pretreatment device 15 through leads; the automatic control system 14 controls the injection amount of the oxidant, the circulating water amount of the flue gas cooler, the inlet water temperature and water amount of the deep catalytic unit, the recirculated flue gas amount and the injection amount of the primary catalyst by combining the load of the boiler furnace, the fuel property and various detection data, monitors the average activity of the primary catalyst and the proportion of high-activity fly ash particles in real time, and timely and thoroughly cleans the dust remover fly ash bin if the average activity or the proportion of the high-activity fly ash particles is lower than 50% -70%, so as to achieve the purpose of automatic control.
Preferentially, the deep catalytic unit 5 is a heat exchanger coated with a desulfurization and denitration catalyst on the surface, an electric heating device 16 is arranged at the inlet of the heat exchanger, the temperature of water at the inlet of the heat exchanger is adjusted by utilizing the power generation of a thermoelectric induction material, and the surface temperature of the deep catalytic unit 5 is in an optimal catalytic temperature range by controlling the flow rate and the temperature of circulating water; the heat exchanger coated with the desulfurization and denitration catalyst on the surface adopts a finned tube heat exchanger, a plate heat exchanger or a light pipe heat exchanger.
Preferably, the deep catalytic unit 5 catalyst is a modified manganese-based, titanium-based or iron-based metal oxide desulfurization and denitrification catalyst.
Preferentially, the oxidant in the oxidant storage tank 3 is ozone, hydrogen peroxide or potassium permanganate, and the molar ratio of the oxidant to the pollutants in the flue gas is 2-4: 1.
preferably, the primary catalyst of the primary catalyst nozzle adopts fly ash power plant waste as the primary catalyst, and the air speed ratio of the primary catalyst is maintained at 6000-20000 h-1(ii) a A primary catalyst nozzle is arranged behind the flue gas cooler 2, a flue gas recirculation port B is arranged behind the induced draft fan 9, and the flue gas is pressurized by the fan 12-1 to convey fly ash to be sprayed into a flue.
Preferably, the flue gas duct between the flue gas cooler 2 and the absorption tower 6 and the dust collector 4 are coated with an oxidation and corrosion resistant coating or lined with a corrosion resistant material.
Preferably, the temperature of the flue gas cooled by the flue gas cooler 2 is controlled to be 160-240 ℃.
Preferably, the thermoelectric induction material laid on the wall surface of the furnace chamber of the boiler 1 is a PbTe system, and is used for meeting the power requirements of an oxidant, circulating water of the deep catalytic unit 5, a primary catalyst supply power device and an automatic control system.
The working method of the desulfurization and denitration flue gas comprehensive treatment device for cooperative thermal power generation comprises the steps that flue gas generated by a boiler 1 passes through a flue gas cooler 2 arranged at a tail flue, the temperature of the flue gas is reduced to 240 ℃, then the flue gas is fully mixed with an injected primary catalyst and an oxidant to achieve the purposes of primary desulfurization and denitration, wherein the oxidant is injected from a nozzle after being pressurized by an oxidant power device 12-3 through an oxidant storage tank 3, the primary catalyst is from fly ash recovered by a dust remover 4, part of the fly ash is roughly treated by a catalyst pretreatment device 15 and then is carried and fed by recirculated flue gas pressurized by a fan 12-1, and the rest of the fly ash is fed to a fly ash storage tank 13; the flue gas, the oxidant and the primary catalyst are fully mixed and reacted and then enter a dust remover 4 for dust removal so as to achieve the aims of partial desulfurization and denitration; then, the flue gas enters a deep catalysis unit 5 consisting of a heat exchanger, the surface of the heat exchanger is coated with an oxidation desulfurization and denitration catalyst, the working medium of the heat exchanger adopts outlet circulating water of a flue gas cooler 2, and the surface temperature of the heat exchanger is controlled by controlling the temperature of inlet circulating water and the temperature of the circulating water, so that the deep catalysis unit 5 is in the optimal reaction working condition, wherein the temperature of the inlet circulating water is controlled by adjusting the power of an electric heating device 16 by using electric energy generated by a thermoelectric induction material laid on the wall surface of a hearth of; then the flue gas enters an absorption tower 6 to separate the oxidized nitrogen oxides and sulfur oxides in time, and the clean flue gas is finally discharged from a chimney 9 through a demister 7 and a flue gas reheater 8; the power required by the flowing of the flue gas is provided by a draught fan 10; in addition, the automatic control system 14 controls the injection amount of the oxidant, the circulating water amount of the flue gas cooler, the inlet water temperature and water amount of the deep catalytic unit, the recirculated flue gas amount and the injection amount of the primary catalyst by combining the load of the boiler furnace, the fuel property and various detection data, monitors the average activity of the primary catalyst and the proportion of high-activity fly ash particles in real time, and timely and thoroughly cleans the dust remover fly ash bin if the average activity or the proportion of the high-activity fly ash particles is lower than 50% -70%, so that the purpose of automatic control is achieved.
Compared with the prior art, the invention has the following advantages:
1) the invention adopts multi-stage catalyst to realize the synergistic desulfurization and denitrification, and most of the catalysts are used for NOXSensitive in concentration, and can preliminarily reduce NO in the flue gas by the primary catalystXConcentration to ensure that the deep catalytic unit is in proper catalytic reaction NOXUnder the concentration working condition.
2) The device and the method have low operation cost. On one hand, the low-cost catalyst such as power plant waste fly ash is used as the primary catalyst, so that the investment and the operating cost of the primary catalytic unit can be reduced. On the other hand, the high temperature of the wall surface of the hearth can create larger temperature difference, improve the power generation efficiency of the thermoelectric induction material and provide enough power supply for the whole system.
3) The primary desulfurization and denitration catalyst, namely the fly ash, is carried by the purified recycled flue gas and sprayed into the flue, so that NO in the original flue gas can be reducedX/SOXThe content of the catalyst is fully mixed with the sprayed oxidant and the flue gas for catalytic oxidation, so that the catalytic oxidation reaction time is greatly prolonged, and the removal efficiency is improved.
4) The deep catalytic unit is arranged in a mode of coating a catalyst on the surface of a finned tube type heat exchanger or a plate type heat exchanger. On the basis of increasing the contact area of the flue gas and the catalyst and the oxidant, the temperature and the water quantity of the inlet water of the heat exchanger of the deep catalytic unit can be adjusted by using the electric energy generated by the heat absorbed by the flue gas cooler or the thermoelectric induction material laid on the wall surface of the hearth, the deep catalytic unit is controlled to be in the optimal reaction condition, the catalytic reaction efficiency is increased, and the defects that the reaction condition cannot be adjusted and the catalytic reaction cannot be in the optimal reaction condition in the prior art are overcome.
5) The invention introduces an automatic control system to monitor the average activity and the high-activity fly ash particle ratio of the primary catalyst in real time, and if the average activity or the high-activity fly ash particle ratio is low, the dust remover fly ash bin is thoroughly cleaned in time to ensure the activity of the primary catalyst. Meanwhile, the automatic control system is used for controlling the injection amount of the oxidant, the circulating water amount of the flue gas cooler, the inlet water temperature and water amount of the deep catalytic unit, the recirculated flue gas amount and the injection amount of the primary catalyst by combining the hearth load, the fuel property and various detection data, so that the high-efficiency operation of the whole flue gas comprehensive treatment system is ensured.
Drawings
FIG. 1 is a schematic diagram of a desulfurization and denitrification flue gas comprehensive treatment device and method for cooperative thermal power generation.
In the figure: 1-a boiler; 2-the smoker cooler 3-the oxidant storage tank; 4-a dust remover; 5-deep catalytic unit; 6-an absorption tower; 7-a demister; 8-a flue gas reheater; 9-a draught fan; 10-a chimney; 11-an electrical storage device; 12-1-a fan; 12-2-Pump I; 12-3-an oxidant power plant; 12-4-pump II; 13-a fly ash storage reservoir; 14-an automatic control system; 15-a catalyst pretreatment unit; 16-electric heating means.
Detailed Description
The construction and operation of the present invention will be further described with reference to the accompanying drawings.
A flue gas cooler 2 is arranged in a flue at the tail part of the boiler 1, a pump I12-2 is arranged at the inlet of the flue gas cooler, an oxidant nozzle and a primary catalyst nozzle are arranged in a flue, which is connected with a dust remover 4, of the flue gas cooler 2, an oxidant storage tank 3 is connected with the oxidant nozzle through a pipeline, an oxidant power device 12-3 is arranged on the pipeline, a deep catalysis unit 5 is arranged in the flue between the dust remover 4 and an absorption tower 6, and a pump II 12-4 and an electric heating device 16 are arranged at the water side inlet of the deep catalysis unit 5; a demister 7 is arranged at the outlet of the absorption tower 6, and a flue between the demister 7 and a chimney 10 is sequentially provided with a flue gas reheater 8, a draught fan 9 and a recirculated flue gas opening B; the recycling flue gas opening B is connected with a primary catalyst nozzle through a flue gas pipeline, a fan 12-1 is arranged on the flue gas pipeline, a fly ash outlet of the dust remover 4 is divided into two paths, one path is communicated with the primary catalyst nozzle through a pipeline, a catalyst pretreatment device 15 is arranged on the pipeline, and the other path is communicated with a fly ash storage tank 13 through a pipeline; in addition, a thermoelectric induction material is laid on the wall surface of a hearth of the boiler 1, the thermoelectric induction material is connected with an electric storage device 11, the electric storage device 11 and an automatic control system 14 are connected with a fan 12-1, a pump I12-2, an oxidant power device 12-3, a pump II 12-4, an electric heating device 16 and a catalyst pretreatment device 15 through leads, wherein the electric storage device 11 is connected with the pump I12-2, the pump II 12-4, the oxidant power device 12-3, the catalyst pretreatment device 15 and the electric heating device 16 through a lead A, the automatic control system 14 is connected with the oxidant power device 12-3, the pump II 12-4 and the electric heating device 16 through a lead C, and the rest of the connections are shown by broken lines in FIG. 1.
The invention relates to a desulfurization and denitrification flue gas comprehensive treatment method for cooperative thermal power generation, which comprises the following steps:
the flue gas generated by a boiler 1 passes through a flue gas cooler 2 arranged on a tail flue, the temperature of the flue gas is reduced to 160-240 ℃, then the flue gas is fully mixed with an injected primary catalyst and an oxidant to achieve the purpose of primary desulfurization and denitration, wherein the oxidant is injected from a nozzle after being pressurized by an oxidant power device 12-3 from an oxidant storage tank 3, the primary catalyst is from fly ash recovered by a dust remover 4, part of the fly ash is carried and fed by recirculated flue gas pressurized by a fan 12-1 after being roughly treated by a catalyst pretreatment device 15, and the rest of the fly ash is fed to a fly ash storage tank 13; the flue gas, the oxidant and the primary catalyst are fully mixed and reacted and then enter a dust remover 4 for dust removal so as to achieve the aims of partial desulfurization and denitration; then, the flue gas enters a deep catalysis unit 5 consisting of a heat exchanger, the surface of the heat exchanger is coated with an oxidation desulfurization and denitration catalyst, the working medium of the heat exchanger adopts outlet circulating water of a flue gas cooler 2, and the surface temperature of the heat exchanger is controlled by controlling the temperature of inlet circulating water and the temperature of the circulating water, so that the deep catalysis unit 5 is in the optimal reaction working condition, wherein the temperature of the inlet circulating water is controlled by adjusting the power of an electric heating device 16 by using electric energy generated by a thermoelectric induction material laid on the wall surface of a hearth of; then the flue gas enters an absorption tower 6 to separate the oxidized nitrogen oxides and sulfur oxides in time, and the clean flue gas is finally discharged from a chimney 9 through a demister 7 and a flue gas reheater 8; the power required by the flowing of the flue gas is provided by a draught fan 10; in addition, the automatic control system 14 controls the injection amount of the oxidant, the circulating water amount of the flue gas cooler, the inlet water temperature and water amount of the deep catalytic unit, the recirculated flue gas amount and the injection amount of the primary catalyst by combining the load of the boiler furnace, the fuel property and various detection data, monitors the average activity of the primary catalyst and the proportion of high-activity fly ash particles in real time, and timely and thoroughly cleans the dust remover fly ash bin if the average activity or the proportion of the high-activity fly ash particles is lower than 50% -70%, so that the purpose of automatic control is achieved. Example 1:
the boiler exhaust gas has the NO concentration of 500ppm and the SO2 concentration of 1000ppm, the oxidant adopts hydrogen peroxide solution, and the molar ratio of hydrogen peroxide to pollutants in the flue gas is 4: 1. the first-stage catalytic air speed ratio is controlled to be 10000h-1Left and right. The concentration of NO in the flue gas is reduced to about 250ppm after catalytic oxidation by using the primary catalyst fly ash and an oxidant, the secondary catalyst adopts a Fe/TiO2 catalyst, the surface temperature of a heat exchanger is controlled at 160 ℃, and the space velocity ratio is controlled at 15000h-1. After NO and SO2 in the flue gas are subjected to two-stage catalytic oxidation and absorption by an absorption tower, the final denitration efficiency is 96 percent, and the desulfurization efficiency is 100 percent.
Example 2:
the boiler exhaust gas has the NO concentration of 500ppm and the SO2 concentration of 1000ppm, the oxidant adopts hydrogen peroxide solution, and the molar ratio of hydrogen peroxide to pollutants in the flue gas is 4: 1. the air speed ratio of the first stage of catalysis is controlled at 6000h-1Left and right. The concentration of NO in the flue gas is reduced to about 200ppm after catalytic oxidation by using the primary catalyst fly ash and the oxidant, the secondary catalyst adopts a commercial titanium dioxide catalyst, the surface temperature of a heat exchanger is controlled to be 160 ℃, and the space velocity ratio is controlled to be 15000h-1. After NO and SO2 in the flue gas are subjected to two-stage catalytic oxidation and absorption by an absorption tower, the final denitration efficiency is 96 percent, and the desulfurization efficiency is 100 percent.
Claims (9)
1. The utility model provides a device is administered in synthesis of SOx/NOx control flue gas of thermal power generation in coordination, includes boiler (1), its characterized in that: a flue gas cooler (2) is arranged in a flue at the tail part of the boiler (1), a pump I (12-2) is arranged at the inlet of the flue gas cooler, an oxidant nozzle and a primary catalyst nozzle are arranged in the flue where the flue gas cooler (2) is connected with a dust remover (4), an oxidant storage tank (3) is connected with the oxidant nozzle through a pipeline, an oxidant power device (12-3) is arranged on the pipeline, a deep catalysis unit (5) is arranged in the flue between the dust remover (4) and an absorption tower (6), and a pump II (12-4) and an electric heating device (16) are arranged at the water side inlet of the deep catalysis unit (5); a demister (7) is arranged at the outlet of the absorption tower (6), and a flue gas reheater (8), an induced draft fan (9) and a recirculated flue gas opening (B) are sequentially arranged in a flue between the demister (7) and a chimney (10); the recycling flue gas opening (B) is connected with the primary catalyst nozzle through a flue gas pipeline, a fan (12-1) is arranged on the flue gas pipeline, a fly ash outlet of the dust remover (4) is divided into two paths, one path is communicated with the primary catalyst nozzle through a pipeline, a catalyst pretreatment device (15) is arranged on the pipeline, and the other path is communicated with a fly ash storage warehouse (13) through a pipeline; in addition, a thermoelectric induction material is laid on the wall surface of a hearth of the boiler (1), the thermoelectric induction material is connected with an electric storage device (11), and the electric storage device (11) and an automatic control system (14) are connected with a fan (12-1), a pump I (12-2), an oxidant power device (12-3), a pump II (12-4), an electric heating device (16) and a catalyst pretreatment device (15) through leads; the automatic control system (14) is used for controlling the injection amount of an oxidant, the circulating water amount of a flue gas cooler, the inlet water temperature and water amount of a deep catalytic unit, the recirculated flue gas amount and the injection amount of a primary catalyst by combining the load of a boiler furnace, the fuel property and various detection data, monitoring the average activity of the primary catalyst and the proportion of high-activity fly ash particles in real time, and timely and thoroughly cleaning a dust remover fly ash bin if the average activity or the proportion of the high-activity fly ash particles is lower than 50% -70%, so that the purpose of automatic control is achieved.
2. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: the deep catalysis unit (5) is a heat exchanger coated with a desulfurization and denitration catalyst on the surface, an electric heating device (16) is arranged at the inlet of the heat exchanger, the temperature of water at the inlet of the heat exchanger is adjusted by utilizing the power generation of a thermoelectric induction material, and the surface temperature of the deep catalysis unit (5) is in an optimal catalysis temperature range by controlling the flow rate and the temperature of circulating water; the heat exchanger coated with the desulfurization and denitration catalyst on the surface adopts a finned tube heat exchanger, a plate heat exchanger or a light pipe heat exchanger.
3. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: the catalyst of the deep catalytic unit (5) is a modified manganese-based, titanium-based or iron-based metal oxide desulfurization and denitrification catalyst.
4. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: the oxidant in the oxidant storage tank (3) is ozone, hydrogen peroxide or potassium permanganate, and the molar ratio of the oxidant to pollutants in the flue gas is (2-4): 1.
5. the desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: the primary catalyst of the primary catalyst nozzle adopts fly ash power plant waste as the primary catalyst, and the air speed ratio of the primary catalyst is maintained at 6000-20000 h-1(ii) a A primary catalyst nozzle is arranged behind the flue gas cooler (2), a flue gas recirculation port B is arranged behind the induced draft fan (9), and the flue gas is pressurized by the fan (12-1) to convey the recirculated flue gas and convey fly ash to be sprayed into the flue.
6. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: and the surfaces of the flue between the flue gas cooler (2) and the absorption tower (6) and the dust remover (4) are coated with an oxidation-corrosion-resistant coating or a lining corrosion-resistant material.
7. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, is characterized in that: the temperature of the flue gas cooled by the flue gas cooler (2) is controlled to be 160-240 ℃.
8. The desulfurization and denitrification flue gas comprehensive treatment device based on cooperative thermal power generation as claimed in claim 1, characterized in that: the thermoelectric induction material laid on the wall surface of the hearth of the boiler (1) is a PbTe system and is used for meeting the power requirements of an oxidant, circulating water of the deep catalytic unit (5), a primary catalyst supply power device and an automatic control system.
9. The working method of the desulfurization and denitrification flue gas comprehensive treatment device for cooperative thermal power generation as recited in any one of claims 1 to 8, is characterized in that:
the method comprises the following steps that smoke generated by a boiler (1) passes through a smoke cooler (2) arranged on a tail flue, the temperature of the smoke is reduced to 160-240 ℃, then the smoke is fully mixed with an injected primary catalyst and an oxidant, and the purposes of primary desulfurization and denitration are achieved, wherein the oxidant is injected from a nozzle after being pressurized by an oxidant power device (12-3) from an oxidant storage tank (3), the primary catalyst is from fly ash recovered by a dust remover (4), part of fly ash is carried and fed by recycled smoke pressurized by a fan (12-1) after being roughly treated by a catalyst pretreatment device (15), and the rest of fly ash is fed to a fly ash storage tank (13); the flue gas, the oxidant and the primary catalyst are fully mixed and reacted and then enter a dust remover (4) for dust removal to achieve the aims of partial desulfurization and denitration; then, the flue gas enters a deep catalysis unit (5) consisting of a heat exchanger, the surface of the heat exchanger is coated with oxidation desulfurization and denitration catalysts, the working medium of the heat exchanger adopts outlet circulating water of a flue gas cooler (2), the surface temperature of the heat exchanger is controlled by controlling the inlet circulating water temperature and the circulating water temperature, so that the deep catalysis unit (5) is in the optimal reaction working condition, wherein the inlet circulating water temperature is controlled by adjusting the power of an electric heating device (16) by using electric energy generated by a thermoelectric induction material laid on the wall surface of a hearth of a boiler (1); then the flue gas enters an absorption tower (6) to separate oxidized nitrogen oxides and sulfur oxides in time, and the clean flue gas is finally discharged from a chimney (9) through a demister (7) and a flue gas reheater (8); the power required by the flow of the flue gas is provided by a draught fan (10); in addition, an automatic control system (14) is combined with the load of a boiler furnace, the fuel property and various detection data to control the injection amount of an oxidant, the circulating water amount of a flue gas cooler, the inlet water temperature and the water amount of a deep catalytic unit, the recirculated flue gas amount and the injection amount of a primary catalyst, the average activity of the primary catalyst and the proportion of high-activity fly ash particles are monitored in real time, and if the average activity or the proportion of the high-activity fly ash particles is lower than 50% -70%, a dust remover fly ash bin is thoroughly cleaned in time, so that the purpose of automatic control is achieved.
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