CN106853327B - Low-temperature flue gas desulfurization and denitrification integrated method and device - Google Patents
Low-temperature flue gas desulfurization and denitrification integrated method and device Download PDFInfo
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- CN106853327B CN106853327B CN201610137024.0A CN201610137024A CN106853327B CN 106853327 B CN106853327 B CN 106853327B CN 201610137024 A CN201610137024 A CN 201610137024A CN 106853327 B CN106853327 B CN 106853327B
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
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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
- B01D53/32—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 electrical effects other than those provided for in group B01D61/00
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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
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, which integrates a plasma desulfurization and denitrification device and hydrogen peroxide catalytic activation and denitrification on a flue to be treatedTwo or three kinds of devices in sulphur denitrification facility and ozone oxidation SOx/NOx control device, in the scheme that contains plasma SOx/NOx control device, plasma SOx/NOx control device sets up in the foremost of flue, and under the circumstances that hydrogen peroxide solution, ozone oxidation SOx/NOx control device coexist, hydrogen peroxide solution catalytic activation SOx/NOx control device is located the front end. The invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, which integrates a plasma desulfurization and denitrification technology and H 2 O 2 Two or three technologies of the catalytic activation technology and the ozone advanced oxidation desulfurization and denitrification technology are applied to one scheme, the three denitrification technologies can be adjusted in a synergistic manner according to different working conditions of flue gas, and NO is increased x The removal efficiency is improved, and the desulfurization and denitrification operation cost is reduced.
Description
Technical Field
The invention relates to a desulfurization and denitrification method and device, in particular to a low-temperature flue gas desulfurization and denitrification integrated method and device.
Background
Nitrogen oxides and sulfur oxides produced by the combustion of fossil fuels are the major components of air pollutants, they can form acid rain and photochemical smog, and can cause severe haze weather, causing great harm to living bodies. Such pollutants have seriously affected human life health and living environment, and therefore, the control and elimination of nitrogen oxide and sulfur oxide emissions is an urgent need.
At present, ammonia selective catalytic reduction denitration (SCR) technology is generally adopted for denitration of high-temperature (300-400 ℃) flue gas, and the technology requires that the flue gas temperature is kept at 300-400 ℃ so as to maintain the activity of a catalyst. Limestone-gypsum Wet Flue Gas Desulfurization (WFGD) technology is generally adopted for desulfurization, the removal efficiency of sulfur oxides is high, but mining of limestone serving as a desulfurizing agent damages mountain bodies, the value of calcium sulfate serving as a desulfurization byproduct is low, the calcium sulfate cannot be utilized, and secondary pollution is caused by mass accumulation.
The main emission sources of nitrogen oxides and sulfur oxides are coal-fired power plants, motor vehicles and industrial vehiclesAn industrial enterprise. The technical improvement of nitrogen oxide emission control of coal-fired power plants and motor vehicles has been basically completed, and the emission control of nitrogen oxides of a large number of industrial enterprises is gradually promoted by the nation. Taking coking flue gas as an example, the current emission standard of pollutants for coking chemical industry (GB 12671-2012) for NO x Has a control value of 200 mg/m 3 (Heat recovery Coke oven) and 500 mg/m 3 (machine coke, semi-coke oven), the emission strict control area of the enterprise is 150 mg/m 3 . At present, about 2000 coke ovens exist nationwide, most of the coke ovens are not provided with flue gas denitration and desulfurization devices, along with the implementation of GB12671-2012, the coke ovens are imperatively provided with the denitration and desulfurization devices, and along with the increase of environmental protection regulation, NO is increased x And SO 2 Will also be referred to as ultra-low emission.
However, no mature denitration technology exists for the coking flue gas, and the technologies which are currently being subjected to engineering demonstration mainly comprise a low-temperature SCR and an oxidation absorption method. The low-temperature SCR catalyst is afraid of sulfur, the concentration fluctuation of nitrogen oxides is large, the ammonia injection amount is difficult to control, and secondary pollution such as serious ammonia leakage is caused. In addition, coal tar in the flue gas easily blocks the catalyst pore channels, so that the catalyst is inactivated. These problems make the oxidation absorption method become the development direction of the denitration and desulfurization of the coking flue gas.
The oxidation absorption method generally uses ozone and hydrogen peroxide as oxidants. The redox potential of ozone is 2.07V, second only to hydroxyl radicals. In the oxidation process, the carried oxygen atoms are used up, the rest is converted into oxygen, and the oxygen enters a stable state, and no secondary pollution is caused in the use process. However, the denitration process has the problems of large dosage and high production cost, and more NO can be generated by reducing the dosage 2 Instead of the higher valence N 2 O 5 Causing difficulty in absorption. The oxydol has strong oxidizability, wide source and low price, is reduced into water after the oxidation process, does not cause environmental pollution, and is a green oxidant. But liquid-phase hydrogen peroxide oxidation denitration is generally used at high temperature of about 500 ℃, at low temperature (<The oxidation activity in the smoke at 280 ℃ is poor and the smoke is not easy to utilize.
CN105013323A reports an integrated system for desulfurization and denitration of coke oven flue gas by adopting an ozone oxidation and hydrogen peroxide liquid activation process, the ozone oxidation process of the system is placed before the hydrogen peroxide process, and sulfur dioxide can be oxidized while ozone oxidation and denitration are performed, so that the operation cost of ozone is high, and the flue gas desulfurization cost is increased.
CN102343212A provides a denitration process combining ozone and hydrogen peroxide with oxidation and wet absorption, the method is to spray hydrogen peroxide solution into boiler flue gas, then spray ozone, oxidize nitric oxide in the flue gas into high-valence nitrogen oxide which is easy to absorb by an oxidant, and finally absorb denitration products by adopting a desulfurization solution. The temperature range of the liquid hydrogen peroxide sprayed by the invention is 100-200 ℃, the activity of the hydrogen peroxide is poor at the temperature, the oxidation efficiency of NO in the flue gas is very low, and the ideal removal effect cannot be achieved.
Disclosure of Invention
The object of the present invention is to solve H 2 O 2 When the oxidized flue gas is simultaneously subjected to desulfurization and denitrification, the utilization efficiency of liquid-phase feeding is low, and H 2 O 2 Insufficient activity; the method and the device for integrating the desulfurization and the denitrification of the low-temperature flue gas have the advantages of solving the problems of high pollutant removal operation cost caused by large using amount, incomplete absorption when the using amount is low and unreasonable arrangement of oxidation procedures when the ozone is used for oxidizing the flue gas.
The invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, which is characterized in that: the method is characterized in that two or three devices of a plasma desulfurization and denitrification device, a hydrogen peroxide catalytic activation desulfurization and denitrification device and an ozone oxidation desulfurization and denitrification device are integrated on a flue to be treated, in the scheme containing the plasma desulfurization and denitrification device, the plasma desulfurization and denitrification device is arranged at the foremost end of the flue, firstly, flue gas in the flue is treated, flue gas molecules are ionized into active particles and free radicals, and SO in the flue gas is oxidized 2 And NO; in pairUnder the condition that the oxygen water catalytic activation desulfurization and denitrification device and the ozone oxidation desulfurization and denitrification device exist simultaneously, the hydrogen peroxide catalytic activation desulfurization and denitrification device is positioned at the front end of the ozone oxidation desulfurization and denitrification device SO as to utilize hydrogen peroxide and hydroxyl radicals to firstly carry out most of SO in the flue gas 2 Removing a small amount of NO, and then utilizing ozone to remove a small amount of SO 2 And most NO are removed, thereby solving the problem of directly removing SO by using ozone 2 The cost is high.
The invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, which is characterized in that hydrogen peroxide dosage in a hydrogen peroxide catalytic activation desulfurization and denitrification device and NO in flue gas x The molar ratio of the ozone to the NO in the flue gas is 0.5-2, and the amount of the ozone in the ozone oxidation desulfurization and denitrification device is equal to that of the NO in the flue gas x The molar ratio of (A) to (B) is 0.2 to 1.
The invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, wherein the voltage and frequency applied by a plasma desulfurization and denitrification device and NO in flue gas x And SO 2 The content of the smoke is in direct proportion, and the temperature of the smoke in the flue is 80-250 ℃.
The invention discloses a low-temperature flue gas desulfurization and denitration integrated method.A plasma desulfurization and denitration device consists of a plasma generator arranged on a flue, and the plasma generator ionizes flue gas in the flue into active particles OH, O and HO 2 And a free radical;
the ozone oxidation desulfurization and denitrification device comprises a gas tank, an adjusting valve and an ozone generator, wherein air or oxygen used as an ozone preparation source is stored in the gas tank, and the adjusting valve is arranged on a pipeline between the gas tank and the ozone generator and used for adjusting the gas flow; ozone generated by the ozone generator is introduced into the flue along the reverse direction of the flow of the flue gas so as to carry out desulfurization and denitrification treatment on the flue gas;
the hydrogen peroxide catalytic activation desulfurization and denitrification device comprises a hydrogen peroxide storage tank, a feed pump, a heater, a gas carrying tank, a fan, a preheater and a catalyst device, wherein the feed pump is used for pumping liquid hydrogen peroxide in the hydrogen peroxide storage tank into the heater, and the heater is used for gasifying part of hydrogen peroxide in the hydrogen peroxide storage tank; the air or inert gas is stored in the gas carrying tank, the fan is used for pumping the gas in the gas carrying tank into the preheater for heating, the carrier gas discharged by the preheater is mixed with the gaseous hydrogen peroxide discharged by the heater and carries the gaseous hydrogen peroxide into the catalyst device, partial hydrogen peroxide is activated into hydroxyl radicals under the action of the catalyst, and the mixed gas containing the hydroxyl radicals, the gaseous hydrogen peroxide and the carrier gas discharged by the catalyst device is introduced into the flue along the reverse direction of the flowing of the flue gas, so that the desulfurization and denitrification treatment of the flue gas is realized.
In the integrated method for low-temperature flue gas desulfurization and denitrification, the mass ratio of the flow of carrier gas discharged from a carrier gas tank to the feed quantity of hydrogen peroxide in the hydrogen peroxide catalytic activation desulfurization and denitrification device is 0.5-1.5.
In the integrated method for low-temperature flue gas desulfurization and denitrification, the periphery of the catalyst device is provided with electric tracing equipment in the hydrogen peroxide catalytic activation desulfurization and denitrification device.
The invention has the beneficial effects that: the invention discloses a low-temperature flue gas desulfurization and denitrification integrated method, which integrates a plasma denitrification technology and H 2 O 2 Two or three technologies of the catalytic activation technology and the ozone advanced oxidation denitration technology are applied to one scheme, the three denitration technologies can be adjusted in a synergistic manner according to different working conditions of flue gas, and NO is increased x The removal efficiency is improved, and the desulfurization and denitrification operation cost is reduced.
Compared with the prior art, the invention has the advantages that:
(1) Denitration technique of plasma, H 2 O 2 The catalytic activation oxidation denitration and ozone advanced oxidation denitration technologies are organically applied together, and the most suitable denitration technology combination is used on different flue parts, so that the desulfurization and denitration capability at low temperature is effectively enhanced;
（2）H 2 O 2 during the catalytic activation oxidation process, the catalyst is firstly vaporized and then activated into hydroxyl free radicals under the action of the catalyst, so that H is increased 2 O 2 The activation efficiency of the catalyst is beneficial to removing nitrogen oxides and sulfur oxides;
(3) H is to be 2 O 2 The desulfurization and denitrification technology is placed in the ozone desulfurization and denitrification technologyBefore, ozone oxidation SO is avoided 2 The problem of high cost caused by desulfurization and denitrification of flue gas is solved;
(4) According to NO in the flue gas x And SO 2 In a synergistic manner, using three denitration techniques, SO 2 The removal rate of the catalyst can reach 100 percent, and NO x The removal rate of the catalyst is over 95 percent.
Drawings
FIG. 1 is a schematic structural diagram of the first embodiment of the present invention;
FIG. 2 is a schematic structural diagram of the second embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a 3 rd embodiment of the present invention;
fig. 4 is a schematic structural diagram of the 4 th embodiment of the present invention.
In the figure: 1 plasma generator, 2 gas tank, 3 regulating valve, 4 ozone generator, 5 flue, 6 absorption tower, 7 hydrogen peroxide storage tank, 8 feed pump, 9 heater, 10 gas carrying tank, 11 blower, 12 preheater, 13 catalyst device and 14 electric heat tracing equipment.
Detailed Description
The invention is further described with reference to the following figures and examples.
Example 1
As shown in fig. 1, which shows a schematic structural diagram of the embodiment 1 in the present invention, the method for integrating desulfurization and denitrification of low-temperature flue gas is composed of a plasma desulfurization and denitrification device and an ozone oxidation desulfurization and denitrification device, the plasma desulfurization and denitrification device is composed of a plasma generator 1, and the plasma generator 1 is arranged at the front end of a flue 5. The ozone oxidation desulfurization and denitrification device is composed of a gas tank 2, an adjusting valve 3 and an ozone generator 4, wherein a cavity or oxygen is stored in the gas tank 2 to serve as a gas source for preparing ozone, and the adjusting valve 3 is arranged on a pipeline between the gas tank 2 and the ozone generator 4 to realize the adjustment of gas flow. Ozone generated by the ozone generator 4 is introduced into the flue along the reverse direction of the flowing of the flue gas so as to carry out desulfurization and denitrification treatment on the flue gas.
In the working process, the flue gas firstly flows through the low-temperature plasma generator 1, and part of the flue gas in the plasma generator 1Flue gas molecules are ionized to generate OH, O and HO 2 And a variety of reactive species and radicals. SO in flue gas duct 2 NO is oxidized to higher order oxides SO by active particles and free radicals 3 、NO 2 With H in the flue gas 2 H is formed after the meeting of O 2 SO 4 And HNO 3 . Then unreacted SO 2 And NO is subsequently oxidized to SO by ozone generated by an ozone generator 3 And NO 2 And finally, the flue gas enters an absorption tower 6 to be absorbed and purified and then is discharged.
Example 2
As shown in fig. 2, which shows a schematic structural diagram of embodiment 2 of the present invention, the method for integrating desulfurization and denitrification of low-temperature flue gas is composed of a plasma desulfurization and denitrification device and a hydrogen peroxide catalytic activation desulfurization and denitrification device, wherein the plasma desulfurization and denitrification device is composed of a plasma generator 1 and is arranged at the front end of a flue. The hydrogen peroxide catalytic activation desulfurization and denitrification device is composed of a hydrogen peroxide storage tank 7, a feed pump 8, a heater 9, a gas carrying tank 10, a fan 11, a preheater 12 and a catalyst device 13, wherein liquid hydrogen peroxide is stored in the hydrogen peroxide storage tank 7, the feed pump 8 is used for pumping the liquid hydrogen peroxide in the hydrogen peroxide storage tank 7 into the heater 9, and the heater 9 is used for heating the hydrogen peroxide to convert part of the liquid hydrogen peroxide into a gas state.
The carrier gas tank 10 stores air or inert gas as carrier gas, the fan 11 is used for introducing the gas in the carrier gas tank 10 into the preheater 12, and the preheater 12 realizes heating of the carrier gas. The heated carrier gas discharged from the preheater 12 is mixed with the gaseous hydrogen peroxide discharged from the heater 9 and enters the catalyst device 13 with the gaseous hydrogen peroxide, and part of the gaseous hydrogen peroxide can be activated into hydroxyl radicals under the action of the catalyst in the catalyst device 13. The mixed gas containing the hydroxyl radical, the gaseous hydrogen peroxide and the carrier gas discharged from the catalyst device 13 is introduced into the flue 5 along the reverse direction of the flow of the flue gas, so that the desulfurization and denitrification treatment of the flue gas is realized. In order to increase the activity of the catalyst in the catalyst device 13, the periphery of the catalyst device 13 is provided with an electric tracing device 14 for heating.
During operation, the flue gas flows through the firstA plasma generator 1, in the plasma generator 1, partial smoke molecules are ionized to generate OH, O and HO 2 And a variety of reactive species and radicals. SO in flue gas duct 2 NO is oxidized to higher order oxides SO by active particles and free radicals 3 、NO 2 With H in the flue gas 2 H is formed after the meeting of O 2 SO 4 And HNO 3 . Then unreacted SO 2 And NO is subsequently oxidized to H by hydrogen peroxide and hydroxyl radical carried by the carrier gas 2 SO 4 And HNO 3 And finally, the flue gas enters an absorption tower, is absorbed and purified and is discharged.
Example 3
As shown in fig. 3, which shows a schematic structural diagram of the 3 rd embodiment of the present invention, the illustrated method for integrating desulfurization and denitrification of low-temperature flue gas is composed of a hydrogen peroxide catalytic activation desulfurization and denitrification device and an ozone oxidation desulfurization and denitrification device, wherein the hydrogen peroxide catalytic activation desulfurization and denitrification device is arranged at the front end of the ozone oxidation desulfurization and denitrification device. The ozone oxidation desulfurization and denitrification device is the same as that in the embodiment 1, and the hydrogen peroxide catalytic activation desulfurization and denitrification device is the same as that in the embodiment 2, and the description is omitted.
In the working process, the flue gas is firstly subjected to hydroxyl free radical and hydrogen peroxide to remove most of SO 2 And a small amount of NO, which solves the subsequent SO removal by ozone 2 Causing high cost problems, then most of the remaining NO and very little SO 2 Oxidized by ozone to be easily absorbed high-valence nitrogen oxide and SO 3 And finally, the flue gas enters an absorption tower, is absorbed and purified by 6 and then is discharged.
Example 4
As shown in fig. 4, a schematic structural diagram of the 4 th embodiment of the present invention is given, and the illustrated integrated method for low-temperature flue gas desulfurization and denitration is composed of a plasma desulfurization and denitration device, a hydrogen peroxide catalytic activation desulfurization and denitration device, and an ozone oxidation desulfurization and denitration device, wherein the plasma desulfurization and denitration device is disposed at the forefront, the hydrogen peroxide catalytic activation desulfurization and denitration device is disposed in the middle, and the ozone oxidation desulfurization and denitration device is disposed at the end.
In the working process, the flue gas firstly flows through the plasma generator 1, and in the plasma generator 1, partial flue gas molecules are ionized to generate OH, O and HO 2 And a variety of reactive species and radicals. SO in flue gas duct 2 NO is oxidized to higher order oxides SO by active particles and free radicals 3 、NO 2 With H in the flue gas 2 H is formed after the meeting of O 2 SO 4 And HNO 3 . Then unreacted SO 2 And NO is subsequently oxidized to H by hydroxyl radicals, hydrogen peroxide and ozone generated by an ozone generator 2 SO 4 、HNO 3 、SO 3 、NO 2 And finally, the flue gas enters an absorption tower, is absorbed and purified and is discharged.
Experimental analysis:
the desulfurization and denitrification experiments are respectively carried out on the four devices, and SO in the flue gas is obtained during the experiments 2 And NO x The concentration is detected by a Kaien 9206 flue gas analyzer produced in England, and SO 2 And NO x The calculation method of the removal rate comprises the following steps:
SO 2 or NO x Removal rate of = (SO) 2 And NO x Inlet concentration-SO 2 And NO x Outlet concentration)/SO 2 And NO x Inlet concentration.
When the device shown in FIG. 1 is used for desulfurization and denitrification, the flue gas temperature is 80-250 ℃. The ratio of the mole number of the used ozone to the mole number of NO in the flue gas is 0.2-1. By adopting the device, SO in the flue gas is measured 2 The removal rate is 90 percent, and the removal rate of NO is more than 80 percent.
When the device shown in FIG. 2 is used for desulfurization and denitrification, the flue gas temperature is 80-250 ℃. H 2 O 2 Concentration of 27.5% -50%, H 2 O 2 The ratio of the mole number to the NO mole number in the flue gas is 0.2-2, the relationship between the amount of air and the amount of hydrogen peroxide is that each standard air carries 0.02-0.3kg of hydrogen peroxide, the air preheating temperature is 110-150 ℃, and H is H 2 O 2 The heating temperature is 80-110 ℃. By adopting the device, SO in the flue gas is measured 2 The removal rate is 95 percent, NOThe removal rate of (A) is more than 85%.
When the device shown in FIG. 3 is used for desulfurization and denitrification, the flue gas temperature is 80-250 ℃. H 2 O 2 Concentration of 27.5% -50%, H 2 O 2 The ratio of the mole number to the NO mole number in the flue gas is 0.2-2, the relationship between the amount of air and the amount of hydrogen peroxide is that each standard air carries 0.02-0.3kg of hydrogen peroxide, the air preheating temperature is 110-150 ℃, and the H is 2 O 2 The heating temperature is 80-110 ℃. The ratio of the mole number of the ozone to the mole number of NO in the smoke is 0.2-1. By adopting the device, SO in the flue gas is measured 2 The removal rate is 95 percent, and the removal rate of NO is more than 90 percent.
When the device shown in FIG. 4 is used for desulfurization and denitrification, the flue gas temperature is 80-250 ℃. The voltage and frequency of the plasma equipment are determined by the concentration of NO in the flue gas. H 2 O 2 Concentration of 27.5% -50%, H 2 O 2 The ratio of the mole number to the NO mole number in the flue gas is 0.2-2, the relationship between the amount of air and the amount of hydrogen peroxide is that each standard air carries 0.02-0.3kg of hydrogen peroxide, the air preheating temperature is 110-150 ℃, and the H is 2 O 2 The heating temperature is 80-110 ℃. The ratio of the mole number of the used ozone to the mole number of NO in the flue gas is 0.2-1. By adopting the device, the measured SO 2 The removal rate is 100 percent, and the removal rate of NO is more than 95 percent.
Therefore, the apparatuses of the embodiments 1, 2, 3 and 4 have high desulfurization and denitrification efficiency, and the desulfurization and denitrification efficiency is the highest when the plasma desulfurization and denitrification apparatus, the hydrogen peroxide catalytic activation desulfurization and denitrification apparatus and the ozone oxidation desulfurization and denitrification apparatus are used simultaneously.
Claims (3)
1. A low-temperature flue gas desulfurization and denitrification integrated method is characterized by comprising the following steps: the plasma desulfurization and denitrification device, the hydrogen peroxide catalytic activation desulfurization and denitrification device and the ozone oxidation desulfurization and denitrification device are integrated on a flue to be treated, in the scheme containing the plasma desulfurization and denitrification device, the plasma desulfurization and denitrification device is arranged at the foremost end of the flue, firstly, the flue gas in the flue is treated, and flue gas molecules are ionized to be activeNeutral particles and free radicals to oxidize SO in flue gas 2 And NO; under the condition that the hydrogen peroxide catalytic activation desulfurization and denitrification device and the ozone oxidation desulfurization and denitrification device exist simultaneously, the hydrogen peroxide catalytic activation desulfurization and denitrification device is positioned at the front end of the ozone oxidation desulfurization and denitrification device SO as to utilize hydrogen peroxide and hydroxyl radicals to firstly carry out most of SO in the flue gas 2 Removing a small amount of NO, and then utilizing ozone to remove a small amount of SO 2 Most NO is removed, SO that the problem of directly removing SO by using ozone is solved 2 The cost is high;
hydrogen peroxide consumption in hydrogen peroxide catalytic activation desulfurization and denitrification device and NO in flue gas x The molar ratio of (3) to (2) is 0.5, and the ozone dosage in the ozone oxidation desulfurization and denitrification device and NO in the flue gas x The molar ratio of (A) to (B) is 0.2 to 1;
the voltage and frequency applied by the plasma desulfurization and denitrification device and NO in the flue gas x And SO 2 The content of the smoke is in direct proportion, and the temperature of the smoke in a flue is 80-250 ℃;
the plasma desulfurization and denitrification device consists of a plasma generator (1) arranged on a flue (5), wherein the plasma generator ionizes flue gas in the flue into active particles OH, O and HO 2 And a free radical;
the ozone oxidation desulfurization and denitrification device consists of a gas tank (2), an adjusting valve (3) and an ozone generator (4), wherein air or oxygen serving as an ozone preparation source is stored in the gas tank, and the adjusting valve is arranged on a pipeline between the gas tank and the ozone generator and used for adjusting the gas flow; ozone generated by the ozone generator is introduced into the flue along the reverse direction of the flow of the flue gas so as to carry out desulfurization and denitrification treatment on the flue gas;
the hydrogen peroxide catalytic activation desulfurization and denitrification device comprises a hydrogen peroxide storage tank (7), a feed pump (8), a heater (9), a gas carrying tank (10), a fan (11), a preheater (12) and a catalyst device (13), wherein the feed pump is used for pumping liquid hydrogen peroxide in the hydrogen peroxide storage tank into the heater, and the heater is used for gasifying part of hydrogen peroxide in the hydrogen peroxide storage tank; the air or inert gas is stored in the gas carrying tank, the fan is used for pumping the gas in the gas carrying tank into the preheater for heating, the carrier gas discharged by the preheater is mixed with the gaseous hydrogen peroxide discharged by the heater and carries the gaseous hydrogen peroxide into the catalyst device, partial hydrogen peroxide is activated into hydroxyl radicals under the action of the catalyst, and the mixed gas containing the hydroxyl radicals, the gaseous hydrogen peroxide and the carrier gas discharged by the catalyst device is introduced into the flue along the reverse direction of the flowing of the flue gas, so that the desulfurization and denitrification treatment of the flue gas is realized.
2. The integrated method for low-temperature flue gas desulfurization and denitration according to claim 1, characterized in that: in the device for catalytic activation, desulfurization and denitrification by hydrogen peroxide, the mass ratio of the flow of carrier gas discharged by the carrier gas tank (10) to the feed quantity of hydrogen peroxide is 0.5-1.5.
3. The integrated method for low-temperature flue gas desulfurization and denitration according to claim 1 or 2, characterized in that: in the hydrogen peroxide catalytic activation desulfurization and denitrification device, electric tracing equipment (14) is arranged on the periphery of a catalyst device (13).
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| CN107355301A (en) * | 2017-07-06 | 2017-11-17 | 华电电力科学研究院 | Peak regulation Gas Generator Set cold start movable type denitration control system and method |
| CN108905407A (en) * | 2018-06-06 | 2018-11-30 | 郭世宏 | The method that compound flue gas desulfurization and denitrification takes off white minimum discharge processing |
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| CN104587813B (en) * | 2015-02-03 | 2017-12-19 | 山东派力迪环保工程有限公司 | A kind of plasma method of denitration of medium small boiler waste gas |
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