CN109745855B - Sintering flue gas SOX、NOXCombined emission reduction system - Google Patents
Sintering flue gas SOX、NOXCombined emission reduction system Download PDFInfo
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Abstract
The invention discloses sintering flue gas SOX、NOxThe combined emission reduction system belongs to the technical field of flue gas treatment. The invention comprises a main flue, a first dust remover, a desulfurization tower, an SCR denitration unit and a chimney; the SCR denitration unit is filled with a honeycomb catalyst module, and the honeycomb catalyst module contains Ce-Mn/TiO2Catalyst, Ce-Mn/TiO2The catalyst consists of a denitration active component and a carrier of the active component, wherein the denitration active component comprises cerium oxide, manganese oxide and ruthenium oxide, and the carrier of the active component is titanium dioxide. The combined emission reduction system firstly treats SO in the sintering flue gasXRemoving, and then realizing NO treatment on the sintering flue gas at the ultralow temperature of 80-120 DEG CxThe denitration device has the advantages of simple structure, reasonable design and easy manufacture, and provides a new idea and technical support for denitration of a large amount of low-temperature, water-containing, sulfur-containing and dust-containing complex flue gas in the steel industry.
Description
Technical Field
The invention belongs to the technical field of flue gas treatment, and particularly relates to sintering flue gas SOX、NOxThe combined emission reduction system.
Background
The steel industry is the prop industry of national economy of China and is also a basic industry, but the steel industry belongs to the high-energy-consumption and high-pollution industry. NOxIs one of the main pollution sources of the atmospheric pollution of steel mills, NO of sintering machinesxEmission amount of total NO of iron and steel plantx50% -60% of the emission, which is NO of steel millxAnd discharging the main unit. NOxCan cause acid rain and photochemical smog pollution, damage the ozone layer, seriously damage the ecological environment and harm the health of human beings. Therefore, in order to realize ultra-low emission as early as possible in the steel industry and reduce NO in steel millsxDischarge is imperative.
At present, the denitration technology of sintering flue gas mainly adopts a selective non-catalytic reduction method (SNCR) used at 800-1000 ℃, a medium-temperature selective catalytic reduction method (SCR) used at 280-420 ℃ and a low-temperature SCR used at 150-200 ℃ and above and requiring low sulfur dioxide concentration, but the technology is difficult to directly transplant due to the characteristics of low temperature of sintering flue gas, sulfur dioxide content and the like. The temperature of sintering flue gas is usually below 150 ℃, and the concentration of sulfur dioxide is mostly 800mg/Nm3-1500 mg/Nm3The smoke temperature after wet desulphurization is more than 50-60 ℃, and the dry desulphurization is carried outThe temperature of the flue gas can reach 70-90 ℃, and the SCR reaction conditions can not be met before and after desulfurization.
Through search, the Chinese invention patent application publication No. CN106257141A, application date: 2016, 9, 28 days, discloses a system for recovering sensible heat of sintering ores and simultaneously denitrating flue gas and a realization method thereof, wherein two paths of sintering flue gas from a sintering machine pass through a dust remover, one path of sintering flue gas exchanges heat with high-temperature sintering ores with the average temperature of 600-1000 ℃ from the sintering machine, is heated to 450-650 ℃, is mixed with the other path of sintering flue gas with the temperature of 100-190 ℃, enters an SCR (selective catalytic reduction) reactor after the temperature reaches 200-400 ℃, is subjected to catalytic reduction reaction in the SCR reactor, so that nitrogen oxides in the sintering flue gas are removed, and the sintering flue gas with the nitrogen oxides removed enters a waste heat boiler for recycling flue gas waste heat. The flue gas denitration system and the flue gas denitration method need to heat sintering flue gas, the sintering flue gas enters the SCR reactor to remove nitrogen oxides when the temperature reaches 200-400 ℃, and although a waste heat boiler is used for recycling waste heat of the sintering flue gas after the nitrogen oxides are removed in the later period, the flue gas denitration system and the flue gas denitration method still have the defects of large energy consumption, complex process, various devices and the like; in addition, the invention does not deeply research the final denitration effect of the flue gas denitration system and the flue gas denitration method.
Chinese invention patent application publication No. CN104174287A, application date: 6/8/2014, the invention discloses a partial flue gas denitration system and a partial flue gas denitration method for a sintering machine, wherein the system comprises a dust remover, a sintering main exhaust fan, a desulfurization device, a desulfurization induced draft fan, a heating device, a denitration induced draft fan, a non-denitration flue and a chimney; through under the effect of sintering main air exhauster and desulfurization draught fan, make sintering machine aircraft nose flue gas discharge port exhaust sintering flue gas get into desulphurization unit through the dust remover, partly get into the flue that does not denitrate in the flue gas after the desulfurization, another part gets into denitrification facility through rising temperature device under the effect of denitration draught fan, then mix through the chimney emission with the flue gas after the desulfurization through the flue that does not denitrate, when emission standard tends to rigorously, can reduce the flue gas volume that gets into the flue that does not denitrate and adjust. In the invention, although the energy consumption and the treatment cost are reduced by the denitration treatment of part of the flue gas, the part of the flue gas entering the denitration device for denitration treatment still needs a heating device for heating, and the temperature is raised to 280-420 ℃ if the denitration device adopts medium-temperature SCR denitration, and is raised to 150-200 ℃ if the denitration device adopts low-temperature SCR denitration.
In order to meet the requirements of desulfurization and denitrification of a large amount of low-temperature, water-containing, sulfur-containing and dust-containing complex flue gas in the steel industry, a system and a method for desulfurization and denitrification of sintering flue gas, which are low in energy consumption, simple in process and good in denitrification effect, are expected to be developed.
Disclosure of Invention
1. Problems to be solved
Aiming at the problems that the sintering flue gas needs to be heated before the sintering flue gas is denitrated by an SCR method in the prior art, and the sintering flue gas can not be denitrated at the ultralow temperature of 80-120 ℃, the invention provides sintering flue gas SOX、NOxThe combined emission reduction system can realize NO treatment on sintering flue gas at ultralow temperature of 80-120 DEG CxThe method provides a new idea and technical support for denitration of a large amount of low-temperature, water-containing, sulfur-containing and dust-containing complex flue gas in the steel industry.
2. Technical scheme
In order to solve the problems, the technical scheme adopted by the invention is as follows:
the invention relates to sintering flue gas SOX、NOxThe combined emission reduction system comprises a main flue, a first dust remover, a desulfurization tower, an SCR denitration unit and a chimney, wherein the first dust remover is arranged on the main flue, the outlet end of the first dust remover is communicated with the chimney through a pipeline, and the desulfurization tower and the SCR denitration unit are sequentially arranged on the pipeline of the first dust remover and the chimney; the SCR denitration unit is filled with a honeycomb catalyst module, and the honeycomb catalyst module contains Ce-Mn/TiO2Catalyst of said Ce-Mn/TiO2The catalyst consists of a denitration active component and a carrier of the active component, wherein the denitration active component comprises cerium oxide, manganese oxide and ruthenium oxide, and the carrier of the active component is titanium dioxide.
Preferably, a second dust remover is further arranged on a pipeline between the desulfurization tower and the SCR denitration unit.
Preferably, the first dust remover and the second dust remover are electrostatic dust removers.
Preferably, a heater is arranged on a pipeline between the second dust remover and the SCR denitration unit.
Preferably, a rectifier is arranged on the top of the SCR denitration unit.
Preferably, an ammonia injection grid is arranged on the pipeline between the heater and the SCR denitration unit, and the ammonia injection grid is used for adding ammonia compounds into the pipeline.
Preferably, the honeycomb catalyst is filled with 3 to 7 layers.
Preferably, Ce-Mn/TiO2The mass percentage of the ruthenium element in the catalyst is 1.14-2.68%.
Preferably, Ce-Mn/TiO2The mass percentage of cerium element in the catalyst is 1.22-2.84%, and the mass percentage of manganese element is 10.42-11.7%.
Preferably, the specific surface area of the honeycomb catalyst is 68-75 m2/g。
3. Advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention relates to sintering flue gas SOX、NOxThe combined emission reduction system comprises a main flue, a first dust remover, a desulfurization tower, an SCR denitration unit and a chimney, wherein a honeycomb catalyst module is filled in the SCR denitration unit, cerium oxide, manganese oxide and ruthenium oxide are taken As denitration active components of the honeycomb catalyst module, titanium dioxide is taken As a carrier of the active components, and ruthenium (Ru) is an element with the largest valence in the world and is resistant to acid, alkali, As and Cl-The corrosion capability is very strong, ruthenium can form a plurality of oxidation states in the denitration process, the surface defects of the catalyst are expanded, the active sites on the surface of the catalyst are increased, and the NO on the surface of the catalyst is further enhancedx、NH3And O2The adsorption and transfer effects of (1), and the denitration temperature of the catalyst are greatly reduced, so that the system can realize the adsorption and transfer effects of (80 to E)NO for sintering flue gas at 120 ℃ and ultralow temperaturexGood removal is carried out;
(2) the invention relates to sintering flue gas SOX、NOxThe SCR denitration unit is filled with 3-7 layers of honeycomb-shaped honeycomb catalyst modules, and the honeycomb catalyst modules contain Ce-Mn/TiO2Catalyst, Ce-Mn/TiO2The catalyst comprises the following components in percentage by mass: 1.22-2.84% of cerium element, 10.42-11.7% of manganese element, 1.14-2.68% of ruthenium element and 45.84-47.02% of titanium element, wherein in order to utilize the activity performance of cerium oxide, manganese oxide and ruthenium oxide and the oxygen supply performance of titanium dioxide to the maximum extent, the mass percentage ratio relation among cerium oxide, manganese oxide, ruthenium oxide and titanium dioxide is deeply researched, so that the denitration effect of the catalyst in the denitration process of sintering flue gas is better;
(3) the invention relates to sintering flue gas SOX、NOxThe rectifier is arranged at the top of the SCR denitration unit, so that the desulfurized sintering flue gas entering the SCR denitration unit through a pipeline can be more uniformly contacted with the honeycomb-shaped honeycomb catalyst module, and NO of the sintering flue gas by the honeycomb catalyst module is fully exertedxUltra-low temperature removal;
(4) the invention relates to sintering flue gas SOX、NOxThe combined emission reduction system has the advantages of simple structure, reasonable design and easy construction.
Drawings
FIG. 1 shows the sintering flue gas SO of the present inventionX、NOxThe structural schematic diagram of the combined emission reduction system;
the reference numerals in the figures illustrate:
100. a main flue; 110. a first dust remover;
200. a desulfurizing tower; 210. a second dust remover; 220. a heater; 230. an ammonia injection grid;
240. a rectifier; 300. an SCR denitration unit; 400. and (4) a chimney.
Detailed Description
The invention is further described with reference to specific examples.
Although these specific embodiments are described in sufficient detail to enable those skilled in the art to practice the invention, it should be understood that other embodiments may be realized and that various changes to the invention may be made without departing from the spirit and scope of the present invention. The following more detailed description of the embodiments of the invention is not intended to limit the scope of the invention, as claimed, but is presented for purposes of illustration only and not limitation to describe the features and characteristics of the invention, to set forth the best mode of carrying out the invention, and to sufficiently enable one skilled in the art to practice the invention. Accordingly, the scope of the invention is to be limited only by the following claims.
Example 1
As shown in FIG. 1, the sintering flue gas SO of the present inventionX、NOxThe combined emission reduction system comprises a main flue 100, a first dust remover 110, a desulfurizing tower 200, an SCR denitration unit 300 and a chimney 400, wherein the main flue 100 is provided with the first dust remover 110, the outlet end of the first dust remover 110 is communicated with the chimney 400 through a pipeline, and the desulfurizing tower 200 and the SCR denitration unit 300 are sequentially arranged on the pipelines of the first dust remover 110 and the chimney 400; a second dust remover 210 is further arranged on a pipeline between the desulfurization tower 200 and the SCR denitration unit 300, and a heater 220 and an ammonia injection grid 230 are sequentially arranged on the pipeline between the second dust remover 210 and the SCR denitration unit 300; the top of the SCR denitration unit 300 is provided with a rectifier 240, the SCR denitration unit 300 is filled with a honeycomb catalyst module, and the honeycomb catalyst module contains Ce-Mn/TiO2A catalyst; the Ce-Mn/TiO2The denitration active component of the catalyst comprises cerium oxide, manganese oxide and ruthenium oxide.
It should be noted that the first dust remover 110 and the second dust remover 210 are both electrostatic dust removers, and are used for performing dust removal treatment on sintering flue gas to prevent smoke from blocking pipelines or subsequent desulfurization and denitration process equipment. The ammonia injection grid 230 is used for adding ammonia gas (or liquid ammonia) into the pipeline to ensure that the catalytic denitration reaction in the SCR denitration unit 300 is smoothly performed; the heater 220 is configured to heat the desulfurized flue gas to ensure that the catalyst in the SCR denitration unit 300 achieves the best denitration effect.
It should be noted that, unlike the prior art, the heater 220 in the system of the present embodiment does not need to heat the desulfurized flue gas to 150 ℃ or higher, but only needs to heat the flue gas to 80-120 ℃, because the honeycomb catalyst module in the subsequent SCR denitration unit 300 can realize NO at an ultralow temperature of 80-120 ℃XThe good removal of the catalyst can ensure the denitration effect and reduce the energy consumption, thereby reducing the process cost.
In addition, the flue gas to be denitrated is sent into the SCR denitration unit 300 by the rectifier 240 arranged on top of the SCR denitration unit 300, and the purpose of the rectifier is to: sintering flue gas after the desulfurization is before getting into SCR denitration unit through the pipeline, because compare with SCR denitration unit 300 internal diameters, the pipeline internal diameter is less relatively, directly get into SCR denitration unit and make sintering flue gas mainly concentrate on the surface at catalyst layer middle part, and can't contact with whole catalyst layer, in order to avoid this kind of condition, set up the sintering flue gas that the rectifier can make after the desulfurization and distribute on whole catalyst layer surface uniformly, ensure sintering flue gas and catalyst fully contact, improve sintering flue gas NO to the improvement, the pipeline internal diameter is less than, directly get into SCR denitration unit and can make sintering flue gas mainly concentrate on the surface at catalyst layer middle part, and can't contact with whole catalyst layer, in order to avoid this kind of a situation, set up the rectifier, sintering flue gas after the desulfurization and distribute on whole catalyst layer surface uniformly, ensure sintering flue gas and catalyst fully contact, improve sintering flue gas NO, the pipeline internal diameter is less thanxThe removal effect of (1).
The SCR denitration unit 300 may be filled with 3 to 7 layers of honeycomb catalyst modules, as shown in fig. 1, in this embodiment, 3 layers of honeycomb catalyst modules are filled. The honeycomb catalyst module is honeycomb-shaped and consists of denitration active components and carriers of the active components, wherein the denitration active components comprise cerium oxide, manganese oxide and ruthenium oxide, and the carriers of the active components are titanium dioxide.
It should be further noted that, the mass percentages of the metal elements of the honeycomb catalyst in the embodiment in the entire catalyst are respectively: 2.44 percent of Ce, 10.74 percent of Mn, 1.14 percent of Ru and 47.02 percent of Ti, wherein the mass percent of the total active elements of Ce, Mn and Ru is 14.32 percent. The specific surface area of the catalyst is 68-75 m2(ii) in terms of/g. The honeycomb catalyst module is prepared by the following steps:
(1) preparation of Ru-Ce-Mn/TiO2Catalyst and process for preparing same
A. 0.038 part of hexahydrate is weighedMixing cerium nitrate and 0.245 part of manganese nitrate tetrahydrate by volume, taking 5 parts of deionized water and 10 parts of absolute ethyl alcohol by volume to form an ethanol aqueous solution, adding cerium nitrate hexahydrate and manganese nitrate tetrahydrate into the ethanol aqueous solution, and uniformly mixing to prepare an active component solution A; then 0.393 part of anatase TiO is weighed2As a carrier, anatase TiO2Adding into the active component solution A, and stirring vigorously for 30 min; heating and stirring the solution after violent stirring in a heat collection type magnetic stirrer at the temperature of 60-70 ℃ for 100min until the solution is evaporated to dryness to obtain a precipitate, and loading the active component solution A on TiO2On a carrier. Grinding the precipitate until no granular sensation exists, and then putting the precipitate into a muffle furnace for roasting, wherein the roasting temperature T1 in the muffle furnace is 500 ℃, and the roasting time is 4h, and finally obtaining the Ce-Mn/TiO2A catalyst powder;
B. weighing 0.38 part of ruthenium nitrosyl nitrate, mixing 5 parts by volume of deionized water and 10 parts by volume of absolute ethyl alcohol to obtain an ethanol aqueous solution, adding the ruthenium nitrosyl nitrate into the ethanol aqueous solution, and uniformly mixing to prepare an active component solution B; then the prepared Ce-Mn/TiO2Adding the catalyst powder into the active component solution B, and violently stirring for 30 min; heating and stirring the solution after violent stirring in a heat collection type magnetic stirrer at the temperature of 60-70 ℃ for 100min until the solution is evaporated to dryness to obtain a precipitate, so that the active component solution B is loaded on Ce-Mn/TiO2On a catalyst. Grinding the precipitate until no granular sensation exists, and then putting the precipitate into a muffle furnace for roasting, wherein the roasting temperature T1 in the muffle furnace is 400 ℃, and the roasting time is 3h, so as to obtain Ru-Ce-Mn/TiO2A catalyst powder; tabletting and screening to obtain 40-60-mesh Ru-Ce-Mn/TiO2Catalyst particles. Wherein when the unit of the mass part pair is g, the volume part corresponds to ml; where the units of parts by mass are kg, parts by volume correspond to L.
(2) Preparation of Honeycomb catalyst Module
According to mass percent, Ru-Ce-Mn/TiO in the step (1)2Mixing a catalyst with 15% of glass fiber, 3% of binder methyl cellulose, 12% of extrusion aid glycerol and 2.5% of pore-expanding agent activated carbon, and then adding 8% of water for bonding; mechanically extruding the bonded mud doughPugging, namely wrapping mud balls subjected to pugging by plastic paper, tightly standing and aging for 24 hours; then the aged mud pie is loaded into an extrusion pipeline and extruded by a grinding tool to prepare the formed honeycomb Ru-Ce-Mn/TiO2A catalyst green body; drying at 105 ℃, and roasting at 300-500 ℃ to obtain the honeycomb catalyst module.
Notably, in the A stage of step (1), the calcination gives Ce-Mn/TiO2The roasting temperature T1 of the catalyst powder is 500 ℃, and in the stage B of the step (1), Ru-Ce-Mn/TiO is obtained by roasting2The calcination temperature T2 of the catalyst particles was 400 ℃, T1 was higher than T2, and the calcination time in the A stage of step (1) was 4 hours and the calcination time in the B stage of step (1) was 3 hours. By adopting the sectional impregnation and roasting mode and designing different roasting temperatures and roasting times, the metal elements reach the maximum oxidation state number, the oxygen storage and release performance is strongest, the maximum utilization of the Ru-Ce-Mn active elements is realized, and the denitration effect of the honeycomb catalyst module is better.
The main principle is as follows: under proper roasting temperature and roasting time, the Lewis acid sites on the surface of the catalyst are the most, the specific surface area and the pore diameter are the largest, the denitration effect is the best, and the optimal Ce-Mn/TiO is prepared by first-stage impregnation and roasting2A catalyst. In addition, Ru is the metal with the most valence state in the world and is resistant to acid, alkali, As and Cl-The corrosion capability is very strong, the oxide surface defect of Ru is the most, and the most stable oxidation state of Ru is RuO2The other oxidation states are unstable, so Ru is converted to RuO2The transition state during the conversion process is particularly important in the catalyst. To convert a large amount of Ru into RuO2And loading the transition state to Ce-Mn/TiO2On the catalyst, the denitration temperature of the catalyst is greatly reduced, the denitration effect and the anti-poisoning performance are obviously improved, the Ru-Ce-Mn/TiO is prepared by adopting the second stage of dipping and roasting and selecting the roasting temperature and time different from the first stage2A catalyst.
The denitration method of the iron ore sintering flue gas combined desulfurization and denitration system comprises the following steps:
s1, flue gas desulfurization
Sintering flue gas generated by the sintering machine enters a first dust remover 110 through a main flue 100 for dust removal treatment, the sintering flue gas after dust removal is sent to the bottom of a desulfurizing tower 200 through an exhaust fan, and the sintering flue gas flows in the desulfurizing tower 200 from bottom to top for semi-dry desulfurization treatment;
s2 and denitration of flue gas
The desulfurized sintering flue gas enters the second dust remover 210 from the top of the desulfurizing tower 200 through a pipeline, dust removal treatment is carried out again, the desulfurized sintering flue gas after dust removal treatment is heated to 80-120 ℃ by the heater 220, ammonia gas (or liquid ammonia) is added into the heated desulfurized sintering flue gas through the ammonia injection grid 230, and the ammonia gas (or liquid ammonia) can be uniformly injected into the pipeline by the ammonia injection grid 230, so that the ammonia gas (or liquid ammonia) can be more fully mixed with the sintering flue gas; then, the flue gas is introduced into the top of the SCR denitration unit 300 through a pipeline, and is sent into the SCR denitration unit 300 through the rectifier 240 arranged at the top of the SCR denitration unit 300, and the inside of the SCR denitration unit 300 is filled with a honeycomb catalyst module containing Ce-Mn/TiO, which is filled with the honeycomb catalyst module2A catalyst; the Ce-Mn/TiO2The denitration active component of the catalyst comprises cerium oxide, manganese oxide and ruthenium oxide. The flue gas is fully contacted with the honeycomb catalyst module for catalytic denitration, and the volume airspeed of sintering flue gas in the SCR denitration unit 300 is 3000-4000/h.
The sintering flue gas SO of the embodiment is usedX、NOxThe combined emission reduction system can realize the denitration efficiency of more than 80% at the ultralow temperature of 80-120 ℃, and greatly reduce the denitration temperature of the catalyst, so that the method can realize the denitration of sintering flue gas NO at the ultralow temperature of 80-120 DEG CxGood removal of the metal oxide.
The invention has been described in detail hereinabove with reference to specific exemplary embodiments thereof. It will, however, be understood that various modifications and changes may be made without departing from the scope of the invention as defined in the appended claims. The detailed description and drawings are to be regarded as illustrative rather than restrictive, and any such modifications and variations are intended to be included within the scope of the present invention as described herein. Furthermore, the background is intended to be illustrative of the state of the art as developed and the meaning of the present technology and is not intended to limit the scope of the invention or the application and field of application of the invention.
Claims (8)
1. Sintering flue gas SOX、NOxThe combined emission reduction system is characterized in that: the flue gas desulfurization device comprises a main flue (100), a first dust remover (110), a desulfurization tower (200), an SCR denitration unit (300) and a chimney (400), wherein the first dust remover (110) is arranged on the main flue (100), the outlet end of the first dust remover (110) is communicated with the chimney (400) through a pipeline, and the desulfurization tower (200) and the SCR denitration unit (300) are sequentially arranged on the pipelines of the first dust remover (110) and the chimney (400); the SCR denitration unit (300) is filled with a honeycomb catalyst module, and the honeycomb catalyst module contains Ce-Mn/TiO2Catalyst of said Ce-Mn/TiO2The catalyst consists of a denitration active component and a carrier of the active component, wherein the denitration active component comprises cerium oxide, manganese oxide and ruthenium oxide, the carrier of the active component is titanium dioxide, and the honeycomb catalyst module is prepared by the following steps:
(1) preparation of Ru-Ce-Mn/TiO2Catalyst and process for preparing same
Preparing active component solution A from cerous nitrate hexahydrate and manganese nitrate tetrahydrate, and preparing active component solution A from anatase TiO2As a carrier, anatase TiO2Adding into the active component solution A, stirring vigorously, and then heating and stirring to make the active component solution A load on TiO2Roasting on a carrier to obtain Ce-Mn/TiO2The roasting temperature T1 of the catalyst is 500 ℃, and the roasting time is 4 h; then, nitrosyl ruthenium nitrate is prepared into an active component solution B, and the prepared Ce-Mn/TiO2Adding the catalyst into the active component solution B, stirring vigorously, and then heating and stirring to load the active component solution B on the Ce-Mn/TiO2On a catalyst, roasting to obtain Ru-Ce-Mn/TiO2The catalyst is calcined at the temperature T2 of 400 ℃ for 3 h;
(2) preparation of Honeycomb catalyst Module
According to mass percent, Ru-Ce-Mn/TiO in the step (1)2Mixing the catalyst with glass fiber, adhesive, extrusion aid and pore-enlarging agent, and adding water for bonding; extruding and pugging the bonded mud dough, tightly wrapping the pugged mud dough with plastic paper, and standing and aging; then extruding and molding the aged mud mass into honeycomb Ru-Ce-Mn/TiO2A catalyst green body; and drying and roasting to obtain the honeycomb catalyst module.
2. Sintering flue gas SO according to claim 1X、NOxThe combined emission reduction system is characterized in that: and a second dust remover (210) is also arranged on a pipeline between the desulfurizing tower (200) and the SCR denitration unit (300).
3. Sintering flue gas SO according to claim 2X、NOxThe combined emission reduction system is characterized in that: the first dust remover (110) and the second dust remover (210) are electrostatic dust removers.
4. Sintering flue gas SO according to claim 2X、NOxThe combined emission reduction system is characterized in that: and a heater (220) is arranged on a pipeline between the second dust remover (210) and the SCR denitration unit (300).
5. Sintering flue gas SO according to claim 1X、NOxThe combined emission reduction system is characterized in that: the top of the SCR denitration unit (300) is provided with a rectifier (240).
6. Sintering flue gas SO according to claim 2X、NOxThe combined emission reduction system is characterized in that: an ammonia injection grid (230) is arranged on a pipeline between the heater (220) and the SCR denitration unit (300), and the ammonia injection grid (230) is used for adding ammonia compounds into the pipeline.
7. Sintering flue gas SO according to claim 1X、NOxIs characterized in thatIn the following steps: the honeycomb catalyst module is filled with 3-7 layers.
8. Sintering flue gas SO according to claim 7X、NOxThe combined emission reduction system is characterized in that: the specific surface area of the honeycomb catalyst is 68-75 m2/g。
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| CN113262630A (en) * | 2021-05-12 | 2021-08-17 | 上海环境卫生工程设计院有限公司 | Denitration equipment for solving problem of high ammonia escape in flue gas of waste incineration plant |
| CN113499774A (en) * | 2021-08-17 | 2021-10-15 | 安徽工业大学 | Preparation method of ruthenium-based high-water-sulfur-resistance sintering flue gas low-temperature denitration catalyst |
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