CN111359408B - Desulfurization and denitration flue gas comprehensive treatment device and method for cooperative thermal power generation - Google Patents
Desulfurization and denitration flue gas comprehensive treatment device and method for cooperative thermal power generation Download PDFInfo
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- CN111359408B CN111359408B CN202010367226.0A CN202010367226A CN111359408B CN 111359408 B CN111359408 B CN 111359408B CN 202010367226 A CN202010367226 A CN 202010367226A CN 111359408 B CN111359408 B CN 111359408B
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- desulfurization
- fly ash
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000003546 flue gas Substances 0.000 title claims abstract description 122
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 37
- 230000023556 desulfurization Effects 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000010248 power generation Methods 0.000 title claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 94
- 239000007800 oxidant agent Substances 0.000 claims abstract description 55
- 230000001590 oxidative effect Effects 0.000 claims abstract description 54
- 239000010881 fly ash Substances 0.000 claims abstract description 47
- 230000003197 catalytic effect Effects 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 230000000694 effects Effects 0.000 claims abstract description 29
- 239000000428 dust Substances 0.000 claims abstract description 28
- 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 13
- 230000003647 oxidation Effects 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 230000002195 synergetic effect Effects 0.000 claims abstract description 6
- 230000005611 electricity Effects 0.000 claims abstract description 3
- 230000001105 regulatory effect Effects 0.000 claims abstract description 3
- 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
- 230000001276 controlling effect Effects 0.000 claims description 7
- 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
- 230000007797 corrosion Effects 0.000 claims description 4
- 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
- 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
- 229910052815 sulfur oxide Inorganic materials 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
- 239000010908 plant waste Substances 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
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical group [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims 1
- 230000003134 recirculating effect Effects 0.000 claims 1
- 238000006555 catalytic reaction Methods 0.000 abstract description 4
- 238000007599 discharging Methods 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
- 239000007789 gas Substances 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000000306 component Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-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
- 150000002696 manganese Chemical class 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—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
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Chimneys And Flues (AREA)
Abstract
The invention discloses a desulfurization and denitration flue gas comprehensive treatment device and method for synergetic thermal power generation, wherein the basic process is that tail flue gas reacts with oxidant and primary catalyst sprayed in a flue, and then dust is removed and NO is partially removed X And SO X Then enters a deep catalytic unit for deep oxidation, and then enters an absorption tower for removing NO X And SO X Demisting, reheating the flue gas and discharging; the wall surface of the hearth is laid with thermoelectric induction materials for generating electricity, so that power is provided for the whole system; the catalyst is arranged in multiple stages, the primary catalyst adopts fly ash, the fly ash is pretreated and sprayed into flue gas for catalytic reaction, the catalyst in the deep catalytic unit adopts high-efficiency desulfurization and denitration catalyst and is coated on the surface of the heat exchanger, the inlet water temperature is regulated by utilizing thermal power generation, and 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, the average activity and the high activity proportion of the primary catalyst are monitored in real time, and the high efficiency and the economical efficiency 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 denitration flue gas comprehensive treatment device and method for synergetic thermal power generation.
Background
Atmospheric pollution is a serious problem that endangers human living environment, SO discharged by coal-fired power plants 2 、NO X Significant harm to human health and ecological environment; wherein SO 2 Is the main reason for forming acid rain, and NOx can generate photochemical smog, destroy ozone layer and generate greenhouse effect. The most mature methods for removing the two pollutants at present 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, and is used for NO and SO 2 The water vapor content is relatively sensitive, and the catalytic efficiency of the catalyst is reduced to different degrees when the concentration of the pollutants is changed. Therefore, in order to economically and efficiently utilize the catalyst to realize the removal of the flue gas pollutants in the coal-fired power plant, the flue gas treatment system of the power plant and the characteristics of the catalyst must be closely combined for consideration. In the existing power station flue gas treatment system, a single catalyst is adopted to remove pollutants, and the relation between the catalyst activity and the change of flue gas components caused by the load change of the power station is not fully considered. Although the traditional flue gas pollutant removal technology has higher removal efficiency, under the condition of intensive economic rapid development, it is extremely important to research an optimization method capable of realizing the catalyst under the condition of removing flue gas pollutants of a power plant at high efficiency.
Disclosure of Invention
In order to overcome the problems of the prior art, the invention aims to provide a method for removing the heat energy in a synergic wayComprehensive treatment device and method for sulfur denitration flue gas, and NO in flue gas can be treated x 、SO 2 And carrying out deep oxidation and removal to realize ultra-clean emission.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
the comprehensive desulfurization and denitration flue gas treatment device for collaborative 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 connected with a dust remover 4 through the flue 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 catalytic 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 catalytic 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 recirculation 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, the 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 the hearth of the boiler 1, the thermoelectric induction material is connected with the electric storage device 11, and the electric storage device 11 and the automatic control system 14 are connected with the fan 12-1, the pump I12-2, the oxidant power device 12-3, the pump II 12-4, the electric heating device 16 and the catalyst pretreatment device 15 through wires; the automatic control system 14 combines the boiler furnace load, the fuel property and all detection data to control the injection quantity of the oxidant, the circulating water quantity of the flue gas cooler, the water temperature and water quantity of the inlet of the deep catalytic unit, the recirculation flue gas quantity and the injection quantity of the primary catalyst, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans the fly ash bin of the dust remover in time 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 the inlet water of the heat exchanger is regulated by utilizing thermoelectric induction materials to generate electricity, and the surface temperature of the deep catalytic unit 5 is in an optimal catalytic temperature range by controlling circulating water flow and temperature; the heat exchanger coated with the desulfurization and denitration catalyst on the surface adopts a fin tube type heat exchanger, a plate type heat exchanger or a light pipe heat exchanger.
Preferably, the catalyst of the deep catalytic unit 5 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 mole ratio of the oxidant to pollutants in the flue gas is 2-4: 1.
preferentially, the primary catalyst of the primary catalyst nozzle adopts fly ash type power plant waste as the primary catalyst, and the space velocity ratio of the primary catalyst is maintained between 6000 and 20000h -1 The method comprises the steps of carrying out a first treatment on the surface of the A primary catalyst nozzle is arranged behind the flue gas cooler 2, a flue gas recirculation port B is selectively arranged behind the induced draft fan 9, and the flue gas is pressurized and recirculated through the fan 12-1 to convey the fly ash to be sprayed into a flue.
Preferably, 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 lining 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 electric 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 integrated desulfurization and denitration flue gas treatment device for the collaborative thermal power generation comprises the steps that flue gas generated by a boiler 1 is cooled to 160-240 ℃ through a flue gas cooler 2 arranged at a tail flue, then the flue gas is fully mixed with an injected primary catalyst and an oxidant, the purpose of preliminary desulfurization and denitration is achieved, the oxidant is injected through a nozzle after being pressurized by an oxidant storage tank 3 through an oxidant power device 12-3, the primary catalyst is from fly ash recovered by a dust remover 4, part of the fly ash is carried and fed into by recycled flue gas after being pressurized by a fan 12-1 after being subjected to rough treatment by a catalyst pretreatment device 15, and the rest of the fly ash is fed into 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 that the aim of partial desulfurization and denitration is fulfilled; then the flue gas enters a deep catalytic unit 5 formed by 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 circulating water at the outlet of the flue gas cooler 2, the surface temperature of the heat exchanger is controlled by controlling the inlet circulating water temperature and the circulating water quantity, so that the deep catalytic unit 5 is in the optimal reaction working condition, and the inlet circulating water temperature is controlled by adjusting the power of an electric heating device 16 through electric energy generated by a thermoelectric induction material laid on the wall surface of a hearth of the boiler 1; the flue gas enters an absorption tower 6 to timely separate oxidized nitrogen oxides and oxidized sulfur oxides, and 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 an induced draft fan 10; in addition, the automatic control system 14 combines the boiler furnace load, the fuel property and all detection data to control the injection quantity of the oxidant, the circulating water quantity of the flue gas cooler, the water temperature and water quantity of the inlet of the deep catalytic unit, the recirculation flue gas quantity and the injection quantity of the primary catalyst, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans the fly ash bin of the dust remover in time 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.
Compared with the prior art, the invention has the following advantages:
1) The invention adopts multistage catalyst to carry out synergistic desulfurization and denitration, and most of the catalyst is used for NO X Concentration sensitivity, the NO in the flue gas can be primarily reduced by the primary catalyst X Concentration to ensure that the deep catalytic unit is in proper catalytic reaction NO X Under the concentration working condition.
2) The device and the method have low running cost. On the one hand, the low-cost catalyst such as the fly ash of the waste of the power plant is used as the primary catalyst, so that the investment and the operation cost of the primary catalytic unit can be reduced. On the other hand, the high temperature of the hearth wall surface can create larger temperature difference, so that the power generation efficiency of the thermoelectric induction material is improved, and enough power supply is provided for the whole system.
3) The primary desulfurization and denitration catalyst, namely fly ash, is carried by the purified recycled flue gas and sprayed into a flue, so that NO in the original flue gas can be reduced X /SO X The 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 improved, and the removal efficiency is improved.
4) The deep catalytic unit is arranged in a mode of coating the surface of a fin-tube heat exchanger or a plate heat exchanger with a catalyst. The method can improve the catalytic reaction efficiency by controlling the deep catalytic unit under the optimal reaction condition on the basis of improving the contact area of the flue gas and the catalyst oxidant and simultaneously utilizing the flue gas cooler to absorb heat or utilizing the electric energy generated by the thermoelectric induction material laid on the wall surface of the hearth to adjust the inlet water temperature and the water quantity of the deep catalytic unit heat exchanger, thereby overcoming the defects that the reaction condition cannot be adjusted and the catalytic reaction cannot be under the optimal reaction condition in the prior art.
5) The invention introduces an automatic control system, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans the fly ash bin of the dust remover in time if the average activity or the proportion of the high-activity fly ash particles is low, so as 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 water temperature and water amount of the inlet of the deep catalytic unit, the recirculation flue gas amount and the injection amount of the primary catalyst by combining with the hearth load, the fuel property and all 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 denitration flue gas comprehensive treatment device and method in cooperation with thermal power generation.
In the figure: 1-a boiler; 2-a flue cooler 3-an oxidant tank; 4-a dust remover; a 5-depth catalytic unit; 6-an absorption tower; 7-a demister; 8-a flue gas reheater; 9-induced draft fan; 10-chimney; 11-an electric storage device; 12-1-fans; 12-2-pump I; 12-3-oxidant power plant; 12-4-pump II; 13-a fly ash repository; 14-an automatic control system; 15-a catalyst pretreatment device; 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 catalytic 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 catalytic 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 recirculation 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, the 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 the furnace chamber of the boiler 1, the thermoelectric induction material is connected with the electric storage device 11, the electric storage device 11 and the automatic control system 14 are connected with the fan 12-1, the pump I12-2, the oxidant power device 12-3, the pump II 12-4, the electric heating device 16 and the catalyst pretreatment device 15 through wires, 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 wires 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 wires C, and the rest of the connection is represented by dotted lines in FIG. 1.
The invention relates to a comprehensive treatment method of desulfurization and denitration flue gas with synergistic thermal power generation, which comprises the following steps:
the flue gas generated by the boiler 1 is cooled to 160-240 ℃ through a flue gas cooler 2 arranged at a tail flue, and then the flue gas is fully mixed with an injected primary catalyst and an oxidant to achieve the purposes of preliminary desulfurization and denitration, wherein the oxidant is injected by a nozzle after being pressurized by an oxidant storage tank 3 through an oxidant power device 12-3, the primary catalyst is derived from fly ash recovered by a dust remover 4, part of fly ash is carried and fed by recycled flue gas after being pressurized by a fan 12-1 after being subjected to coarse treatment by a catalyst pretreatment device 15, and the rest of fly ash is sent to a fly ash storage warehouse 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 that the aim of partial desulfurization and denitration is fulfilled; then the flue gas enters a deep catalytic unit 5 formed by 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 circulating water at the outlet of the flue gas cooler 2, the surface temperature of the heat exchanger is controlled by controlling the inlet circulating water temperature and the circulating water quantity, so that the deep catalytic unit 5 is in the optimal reaction working condition, and the inlet circulating water temperature is controlled by adjusting the power of an electric heating device 16 through electric energy generated by a thermoelectric induction material laid on the wall surface of a hearth of the boiler 1; the flue gas enters an absorption tower 6 to timely separate oxidized nitrogen oxides and oxidized sulfur oxides, and 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 an induced draft fan 10; in addition, the automatic control system 14 combines the boiler furnace load, the fuel property and all detection data to control the injection quantity of the oxidant, the circulating water quantity of the flue gas cooler, the water temperature and water quantity of the inlet of the deep catalytic unit, the recirculation flue gas quantity and the injection quantity of the primary catalyst, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans the fly ash bin of the dust remover in time 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. Embodiment case 1:
the concentration of NO in the boiler exhaust gas is 500ppm, the concentration of SO2 is 1000ppm, the oxidant adopts hydrogen peroxide solution, and the mole ratio of hydrogen peroxide to pollutants in the exhaust gas is 4:1. the first-stage catalytic air speed ratio is controlled to 10000h -1 Left and right. By passing throughThe concentration of NO in the flue gas is reduced to about 250ppm after the catalytic oxidation of the primary catalyst fly ash and the oxidant, the second-stage catalyst adopts Fe/TiO2 catalyst, the surface temperature of the heat exchanger is controlled at 160 ℃, and the airspeed 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%, and the desulfurization efficiency is 100%.
Embodiment case 2:
the concentration of NO in the boiler exhaust gas is 500ppm, the concentration of SO2 is 1000ppm, the oxidant adopts hydrogen peroxide solution, and the mole ratio of hydrogen peroxide to pollutants in the exhaust gas is 4:1. the first-stage catalytic air speed ratio is controlled to 6000h -1 Left and right. The concentration of NO in the flue gas is reduced to about 200ppm after the catalytic oxidation by the primary catalyst fly ash and the oxidant, the secondary catalyst adopts a commercial titanium dioxide catalyst, the surface temperature of the heat exchanger is controlled at 160 ℃, and the airspeed 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%, and the desulfurization efficiency is 100%.
Claims (8)
1. The utility model provides a desulfurization denitration flue gas comprehensive treatment device of cooperation thermal power generation, 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 connected with a dust remover (4) through a pipeline, 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 catalytic 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 catalytic 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 recirculating flue gas opening (B) are sequentially arranged in a flue between the demister (7) and a chimney (10); the recirculation 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, the 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 wires; the automatic control system (14) combines the boiler hearth load, the fuel property and all detection data to control the injection quantity of the oxidant, the circulating water quantity of the flue gas cooler, the water temperature and water quantity of the inlet of the deep catalytic unit, the recirculation flue gas quantity and the injection quantity of the primary catalyst, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans a fly ash bin of the dust remover in time 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;
the deep catalytic unit (5) is a heat exchanger with a desulfurization and denitration catalyst coated on the surface, an electric heating device (16) is arranged at the inlet of the heat exchanger, the water temperature at the inlet of the heat exchanger is regulated by utilizing thermoelectric induction materials to generate electricity, and the surface temperature of the deep catalytic unit (5) is in an optimal catalytic temperature range by controlling circulating water flow and temperature; the heat exchanger coated with the desulfurization and denitration catalyst on the surface adopts a fin tube type heat exchanger, a plate type heat exchanger or a light pipe heat exchanger;
the primary catalyst of the primary catalyst nozzle adopts fly ash type power plant waste as the primary catalyst.
2. The desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to claim 1, which is characterized in that: the deep catalytic unit (5) catalyst is a modified manganese-based, titanium-based or iron-based metal oxide desulfurization and denitrification catalyst.
3. The desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to claim 1, which is characterized in that: the oxidant in the oxidant storage tank (3) is ozone, hydrogen peroxide or potassium permanganate, and the mole ratio of the oxidant to pollutants in the flue gas is (2-4): 1.
4. the desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to claim 1, which is characterized in that: the space velocity ratio of the primary catalyst is maintained between 6000 and 20000h -1 The method comprises the steps of carrying out a first treatment on the surface of the A primary catalyst nozzle is arranged behind the flue gas cooler (2), a flue gas recirculation port B is selectively arranged behind the induced draft fan (9), and the flue gas is pressurized and recirculated through the fan (12-1) to convey the fly ash to be sprayed into a flue.
5. The desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to claim 1, which is characterized in that: and the surfaces of a flue between the flue gas cooler (2) and the absorption tower (6) and the dust remover (4) are coated with an oxidation-resistant corrosion-resistant coating or lining corrosion-resistant material.
6. The desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to 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 ℃.
7. The desulfurization and denitration flue gas comprehensive treatment device for collaborative thermal power generation according to claim 1, which is 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 a deep catalytic unit (5), a primary catalyst supply power device and an automatic control system.
8. The working method of the desulfurization and denitration flue gas comprehensive treatment device for synergetic thermal power generation according to any one of claims 1 to 7 is characterized in that:
the flue gas generated by the boiler (1) is cooled to 160-240 ℃ through a flue gas cooler (2) arranged at a tail flue, then the flue gas is fully mixed with the primary catalyst and the oxidant sprayed in to achieve the purpose of preliminary desulfurization and denitration, wherein the oxidant is sprayed in through a nozzle after being pressurized by an oxidant storage tank (3) through an oxidant power device (12-3), the primary catalyst is from fly ash recovered by a dust remover (4), part of fly ash is carried and fed in by recycled flue gas after being pressurized by a fan (12-1) after being subjected to coarse treatment by a catalyst pretreatment device (15), and the rest of fly ash is sent to a fly ash storage warehouse (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 that the aim of partial desulfurization and denitration is fulfilled; then the flue gas enters a deep catalytic unit (5) formed by 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 circulating water at the outlet 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 quantity, so that the deep catalytic unit (5) is in the optimal reaction working condition, and the inlet circulating water temperature is controlled by adjusting the power of an electric heating device (16) by utilizing 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 timely separate oxidized nitrogen oxides and sulfur oxides, and clean flue gas is finally discharged from a chimney (10) through a demister (7) and a flue gas reheater (8); the power required by the flow of the flue gas is provided by an induced draft fan (9); in addition, an automatic control system (14) combines the boiler hearth load, the fuel property and all detection data to control the injection quantity of the oxidant, the circulating water quantity of the flue gas cooler, the water temperature and water quantity of the inlet of the deep catalytic unit, the recirculation flue gas quantity and the injection quantity of the primary catalyst, monitors the average activity of the primary catalyst and the proportion of the high-activity fly ash particles in real time, and thoroughly cleans a fly ash bin of the dust remover in time 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.
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