CN115957620A - Reaction equipment for reducing CO emission in flue gas and energy-saving emission-reducing method - Google Patents
Reaction equipment for reducing CO emission in flue gas and energy-saving emission-reducing method Download PDFInfo
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- CN115957620A CN115957620A CN202211696561.0A CN202211696561A CN115957620A CN 115957620 A CN115957620 A CN 115957620A CN 202211696561 A CN202211696561 A CN 202211696561A CN 115957620 A CN115957620 A CN 115957620A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 239000003546 flue gas Substances 0.000 title claims abstract description 156
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 95
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000005245 sintering Methods 0.000 claims abstract description 77
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000002485 combustion reaction Methods 0.000 claims abstract description 66
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 35
- 238000007084 catalytic combustion reaction Methods 0.000 claims abstract description 5
- 238000000576 coating method Methods 0.000 claims description 23
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 18
- 230000003197 catalytic effect Effects 0.000 claims description 18
- 229910052751 metal Inorganic materials 0.000 claims description 11
- 239000002184 metal Substances 0.000 claims description 11
- 239000011248 coating agent Substances 0.000 claims description 8
- 238000012544 monitoring process Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 238000009766 low-temperature sintering Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 7
- 229910000831 Steel Inorganic materials 0.000 abstract description 3
- 239000010959 steel Substances 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 7
- 239000010410 layer Substances 0.000 description 5
- 238000006722 reduction reaction Methods 0.000 description 5
- 238000010531 catalytic reduction reaction Methods 0.000 description 4
- 239000011247 coating layer Substances 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 3
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 3
- 229910001928 zirconium oxide Inorganic materials 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 230000010718 Oxidation Activity Effects 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical group [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 1
- 229910000420 cerium oxide Inorganic materials 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
A reaction device for reducing the emission of CO in flue gas and an energy-saving and emission-reducing method comprise a CO energy-saving and emission-reducing pipeline; the CO energy-saving emission-reducing pipeline is sequentially connected with a first heat exchange side of the GGH heat exchanger, a combustion catalyst, a second heat exchange side of the GGH heat exchanger and a flue gas output pipeline through a sintering flue gas input pipeline; and when sintering flue gas of the CO energy-saving emission-reducing pipeline passes through the combustion catalyst, the palladium catalyst catalyzes CO to carry out combustion reaction, and CO combustion of the sintering flue gas improves the flue gas temperature in the SCR reaction tower and high-temperature flue gas enters the second heat exchange side of the GGH heat exchanger so that the sintering flue gas at the first heat exchange side of the GGH heat exchanger has high flue gas temperature on the premise of entering the SCR reaction tower. The invention utilizes the catalytic combustion of combustible CO in the sintering flue gas at a lower temperature of 250-300 ℃, reduces the consumption of blast furnace gas, effectively reduces the CO emission of the sintering flue gas, and is a new breakthrough in energy conservation and emission reduction in the steel sintering industry.
Description
Technical Field
The invention relates to the technical field of emission reduction and recycling in sintering flue gas treatment, in particular to reaction equipment for reducing CO emission in flue gas and an energy-saving emission reduction method.
Background
The sintering flue gas adopts conventional SCR method denitration, after undergoing desulfurization, the flue gas is heated through GGH heat exchanger heat exchange, the hot blast stove is used for heating, the flue gas enters the reaction tower after being heated, the flue gas is in contact reaction with two layers of catalytic reactors, nitrogen oxide is in catalytic reduction reaction, simultaneously, high-temperature flue gas continuously heats the heat exchanger, the heat exchanger continuously heats the raw flue gas, because the flue gas to be treated is generated by the combustion of fuel, because the insufficient combustion and the fuel can not be completely and fully combusted, therefore, the flue gas all contains a certain amount of carbon monoxide, the carbon monoxide is discharged to the atmosphere along with the flue gas, and the environmental protection is not facilitated.
In the prior art, the national emission standard of carbon monoxide is not specifically specified at present, so that the flue gas to be treated is directly discharged after being subjected to desulfurization and denitrification treatment, and the carbon monoxide in the flue gas is not specifically treated and utilized, so that the carbon monoxide is directly discharged. Therefore, the direct emission of carbon monoxide is very polluting to the environment.
Disclosure of Invention
Aiming at the problems of environmental pollution caused by direct emission of CO and ineffective utilization of CO, the invention provides reaction equipment and an energy-saving and emission-reducing method for reducing the emission of CO in flue gas.
In order to achieve the purpose, the invention adopts the following technical scheme: a reaction device for reducing the emission of CO in flue gas comprises an SCR (selective catalytic reduction) reaction tower and a GGH (gas-gas heater) heat exchanger for denitration treatment of sintering flue gas, and further comprises a CO energy-saving emission-reducing pipeline;
the CO energy-saving emission-reducing pipeline is sequentially connected with a first heat exchange side of the GGH heat exchanger, a combustion catalyst, a second heat exchange side of the GGH heat exchanger and a flue gas output pipeline through a sintering flue gas input pipeline;
the combustion catalyst is arranged in the SCR reaction tower, and is filled with palladium catalyst so that the palladium catalyst catalyzes CO to generate combustion reaction at the temperature of 250-300 ℃ when the sintering flue gas of the CO energy-saving emission-reducing pipeline passes through the combustion catalyst, the CO combustion of the sintering flue gas improves the flue gas temperature in the SCR reaction tower, and the high-temperature flue gas enters the second heat exchange side of the GGH heat exchanger so that the sintering flue gas at the first heat exchange side of the GGH heat exchanger has high flue gas temperature before entering the SCR reaction tower.
As a further improvement of the invention: a direct combustion device is arranged between a first heat exchange side of a GGH heat exchanger of the CO energy-saving emission-reducing pipeline and the SCR reaction tower, and is provided with a temperature sensor at a flue gas inlet of the SCR reaction tower and the first heat exchange side of the GGH heat exchanger, and is used for monitoring the sintering flue gas temperature before entering the SCR reaction tower.
As a further improvement of the invention: the temperature of the sintering flue gas in the SCR reaction tower for carrying out normal nitrogen oxide catalytic reaction is 280-300 ℃.
As a further improvement of the invention: and after the flue gas enters the second heat exchange side of the GGH heat exchanger, CO of the sintering flue gas is combusted, and the heat exchange temperature of the first heat exchange side of the GGH heat exchanger is increased by more than 30 ℃ so that the temperature of the combustion flue gas passing through the first heat exchange side of the GGH heat exchanger is increased to 280 ℃.
As a further improvement of the invention: the combustion catalyst is coated with palladium catalysts, the palladium catalysts at least comprise catalytic activity coatings and palladium metal coatings, the catalytic activity coatings are coated on the walls of the flow channels of the combustion catalyst, the palladium metal coatings are formed by coating palladium metal liquid on the catalytic activity coatings and drying the palladium metal liquid, and the catalytic activity coatings respectively comprise active oxides catalytically activated by palladium.
On the other hand, the invention also adopts the following technical scheme: an energy-saving emission-reducing method for reducing CO emission in flue gas comprises the following steps:
sintering flue gas enters a first heat exchange side of the GGH heat exchanger from a sintering flue gas input pipeline to carry out heat exchange and raise the temperature to a reaction temperature;
catalyzing CO by a palladium catalyst at a reaction temperature state to perform a combustion reaction when sintering flue gas in the SCR reaction tower passes through a combustion catalyst;
the CO combustion reaction improves the temperature of the flue gas in the SCR reaction tower, and the high-temperature flue gas exchanges heat with the sintering flue gas at the first heat exchange side of the GGH heat exchanger when passing through the second heat exchange side of the GGH heat exchanger, so that the sintering flue gas can be heated to the reaction temperature required by the SCR denitration reaction;
the high-temperature flue gas is discharged from the flue gas output pipeline after being subjected to catalytic combustion and combustion heat exchange of the CO energy-saving emission-reducing pipeline, and the CO content in the discharged flue gas is reduced by 60-70%.
As a further improvement of the invention: also comprises the following steps:
a direct combustion device is arranged between a first heat exchange side of a GGH heat exchanger of the CO energy-saving emission-reducing pipeline and the SCR reaction tower;
monitoring the reaction temperature before the sintering flue gas enters the SCR reaction tower and the heat exchange temperature of the first heat exchange side of the GGH heat exchanger, and comparing:
when the heat exchange temperature is lower than the reaction temperature, starting the direct combustion device to heat the sintering flue gas flowing through to the reaction temperature;
when the heat exchange temperature is equal to or higher than the reaction temperature, the direct-combustion device is stopped to save energy.
As a further improvement of the invention: the palladium catalyst catalyzes CO to carry out combustion reaction at the reaction temperature of 280-300 ℃.
As a further improvement of the invention: when the high-temperature flue gas passes through the second heat exchange side of the GGH heat exchanger, the high-temperature flue gas exchanges heat with the sintering flue gas at the first heat exchange side of the GGH heat exchanger to enable the heat exchange temperature to be increased by more than 30 ℃, and the original heat exchange temperature at the first heat exchange side of the GGH heat exchanger is increased to 280 ℃ required by SCR denitration reaction.
Compared with the prior art, the invention has the following beneficial effects:
according to the invention, the combustible CO in the sintering flue gas is catalyzed and combusted by using the palladium catalyst at a lower temperature of 250-300 ℃, the combustion reaction can improve the reaction temperature in the tower, the temperature of the sintering flue gas before denitration treatment can be further improved by using the GGH heat exchanger, the consumption of blast furnace gas is reduced, the CO emission amount of the sintering flue gas is effectively reduced, and the method is a new breakthrough in energy conservation and emission reduction in the steel sintering industry.
Drawings
In order to more clearly illustrate the technical solution, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a schematic diagram of a CO energy-saving emission-reducing pipeline structure.
Detailed Description
In order to clearly and completely understand the technical solution, the invention is further described by combining the embodiment with the accompanying drawings, and obviously, the described embodiment is only a part of the embodiment of the invention, and all other embodiments obtained by persons skilled in the art without creative efforts belong to the protection scope of the invention.
It will be understood that the terms "comprises" and/or "comprising," when used in this specification and the appended claims, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof.
It is also to be understood that the terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in the specification of the present invention and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
It should be further understood that the term "and/or" as used in this specification and the appended claims refers to and includes any and all possible combinations of one or more of the associated listed items.
As shown in fig. 1, a reaction device for reducing CO emission in flue gas comprises an SCR reaction tower 100 and a GGH heat exchanger 200 for denitration treatment of sintering flue gas, and further comprises a CO energy-saving emission-reducing pipeline;
the CO energy-saving emission-reducing pipeline is sequentially connected with a first heat exchange side 210 of the GGH heat exchanger, a combustion catalyst 110, a second heat exchange side 220 of the GGH heat exchanger and a flue gas output pipeline 400 through a sintering flue gas input pipeline 300;
the combustion catalyst 110 is arranged in the SCR reaction tower 100, and a palladium catalyst is filled in the combustion catalyst, so that when sintering flue gas of the CO energy saving and emission reduction pipeline passes through the combustion catalyst, the palladium catalyst catalyzes CO to perform combustion reaction at 250-300 ℃, CO combustion of the sintering flue gas improves flue gas temperature in the SCR reaction tower 100, and high-temperature flue gas enters the second heat exchange side 220 of the GGH heat exchanger, so that the sintering flue gas at the first heat exchange side 210 of the GGH heat exchanger has high flue gas temperature before entering the SCR reaction tower.
The temperature of the sintering flue gas in the SCR reaction tower for carrying out normal nitrogen oxide catalytic reaction is 280-300 ℃, the sintering flue gas at about 280 ℃ in the SCR reaction tower carries out normal nitrogen oxide catalytic reaction, and when the sintering flue gas passes through a combustion catalyst, CO in the flue gas is subjected to combustion reaction, and the combustion heat can improve the temperature of the flue gas.
And after the flue gas enters the second heat exchange side of the GGH heat exchanger, the CO of the sintering flue gas is combusted, the heat exchange temperature of the first heat exchange side of the GGH heat exchanger is increased by more than 30 ℃ so that the temperature of the burning flue gas passing through the first heat exchange side of the GGH heat exchanger is increased to 280 ℃, and the original flue gas passing through the first heat exchange side of the GGH heat exchanger can be increased by more than 30 ℃ by the high-temperature flue gas through the GGH heat exchanger. The present embodiment is shown as 180m 2 SCR denitration of sintering machine flue gas is taken as an example, and 14000Nm consumed by hot blast stove per hour is needed 3 4 blast furnace gas (calorific value 3800 KJ/Nm) 3 ) 65 ten thousand meters 3 And heating the sintering flue gas from 250 ℃ to 280 ℃ after heat exchange of GGH for denitration reaction. After the CO energy-saving emission-reducing pipeline of the embodiment is applied, CO in the sintering flue gas is combusted to release heat, the reaction temperature of the flue gas can be increased by more than 30 ℃, namely the temperature of the flue gas at 250 ℃ after the flue gas passes through the first heat exchange side of the GGH heat exchanger is directly increased to about 280 ℃, a direct combustion device or a hot blast stove is not required to be additionally used for reheating the flue gas, and 14000Nm blast furnace gas can be saved per hour 3 Saving blast furnace gas by 1.2 hundred million Nm each year 3 The coal is saved by 1.4 million tons (the calorific value of the coal is 7600 KJ/Kg) every year.
As a further preferable example of the embodiment, a direct combustion device 500 is arranged between the first heat exchange side of the GGH heat exchanger of the CO energy saving and emission reduction pipeline and the SCR reaction tower, and the direct combustion device 500 is provided with a temperature sensor 510 at a flue gas inlet of the SCR reaction tower and the first heat exchange side of the GGH heat exchanger, and is used for monitoring the temperature of sintering flue gas before entering the SCR reaction tower. Sintering flue gas temperature before entering the SCR reaction tower is subjected to heat supplementing through monitoring the sintering flue gas temperature, so that stable catalytic desulfurization reaction temperature in the tower is effectively maintained, fluctuation of reaction temperature is reduced, and desulfurization reaction efficiency of the sintering flue gas is guaranteed.
The embodiment selects the combustion catalyst filled with the palladium catalyst to be configured in the SCR reaction tower, can react in a lower environment of 250-300 ℃, and can further reduce the ignition temperature of the sintering flue gas and improve the temperature stability by directly catalyzing and burning CO in the flue gas at a lower environment temperature of 250-300 ℃ compared with the traditional heat accumulating type catalytic combustion (RCO) of which the reaction temperature is 350-450 ℃ and the reaction temperature of a heat accumulating type thermal incinerator (RTO) of which the reaction temperature is 650 ℃. It should be noted that, the catalytic reduction of the sintering flue gas by using a catalyst is conventionally performed to remove nitrogen oxides to generate molecular nitrogen and water vapor, however, NO and NH existing in the flue gas 3 、SO 2 And H 2 O can have an impact on the catalytic oxidation reaction of CO, which further affects the stability of the catalyst, specifically: during the reaction, NO, NH 3 Competitive adsorption with CO is generated, and the efficiency of CO oxidation reaction is reduced; SO (SO) 2 Part of CO is adsorbed on the surface of the catalyst after entering a reaction system and occupies active sites, so that CO cannot be effectively adsorbed on the catalyst for reaction; h 2 O is adsorbed on the surface of the catalyst after entering a reaction system, and covers part of active sites.
Therefore, the CO catalytic oxidation activity of the traditional catalyst is lower within 120-300 ℃, and NO and H are generated 2 O occupies active sites and combines with metal ions to generate sulfate and nitrate, so that CO cannot combine with the active sites, thereby preventing CO catalytic oxidation reaction from occurring, which cannot be carried out in a low environment of 250-300 ℃. The CO in the embodiment is combusted and catalyzed by using the catalyst, and compared with the catalytic reduction reaction of the traditional catalyst on the CO, the embodiment directly combusts the CO to reduce emission, can raise the temperature in the tower and improve the temperature of sintering flue gas before entering the SCR reaction tower through the GGH heat exchanger, and has the effect of saving energy.
As preferred for this embodiment: the combustion catalyst is coated with a palladium catalyst, the palladium catalyst at least comprises a catalytic activity coating or two layers of catalytic activity coatings in a laminated mode and a palladium metal coating, the catalytic activity coating is coated on the wall part of a flow channel of the combustion catalyst, the palladium metal coating is formed by coating palladium metal liquid on the catalytic activity coating and drying, and the one or two layers of catalytic activity coatings respectively comprise active oxides catalytically activated by palladium. As a further option of this embodiment, when two layered catalytically active coatings are selected and applied on the walls of the flow channels of the combustion catalyst layer by layer, the content of the catalytically active coating layer far away from the walls of the flow channels is higher than the content of the oxide of the catalytically active coating layer applied on the walls, for example, when the oxide is cerium/zirconium oxide, the content of the zirconium oxide of the outer catalytically active coating layer is higher than the content of the zirconium oxide of the catalytically active coating layer applied on the walls.
On the other hand, the invention also provides another implementation case:
an energy-saving emission-reducing method for reducing CO emission in flue gas comprises the following steps:
when the system starts, sintering flue gas enters a first heat exchange side of a GGH heat exchanger from a sintering flue gas input pipeline to perform heat exchange and raise the temperature to a reaction temperature, a direct combustion device and the GGH heat exchanger are required to do work, and the sintering flue gas passing through the first heat exchange side of the GGH heat exchanger reaches 250 ℃;
when sintering flue gas in the SCR reaction tower passes through the combustion catalyst, the palladium catalyst catalyzes CO to generate combustion reaction at the reaction temperature of 250-300 ℃, and the palladium catalyst can catalyze CO in the flue gas to generate combustion reaction at the temperature of more than 150 ℃ to release heat (the temperature of the flue gas in the SCR reaction tower is about 280 ℃). And when passing through the second heat exchange side of the GGH heat exchanger, the high-temperature flue gas exchanges heat with the sintering flue gas at the first heat exchange side of the GGH heat exchanger to increase the heat exchange temperature to more than 30 ℃, and the original heat exchange temperature of 250 ℃ at the first heat exchange side of the GGH heat exchanger is increased to 280 ℃ required by the SCR denitration reaction.
The high-temperature flue gas is discharged from the flue gas output pipeline after being subjected to catalytic combustion and combustion heat exchange of the CO energy-saving emission-reducing pipeline, and the CO content in the discharged flue gas is reduced by 60-70%.
In the operation process of the system, the reaction temperature before the sintering flue gas enters the SCR reaction tower and the heat exchange temperature of the first heat exchange side of the GGH heat exchanger are obtained and compared:
when the heat exchange temperature is lower than the reaction temperature, starting the direct combustion device to heat the sintering flue gas flowing through to the reaction temperature; when the heat exchange temperature is equal to or higher than the reaction temperature, the direct-combustion device is stopped to save energy.
Yangchunxin iron and steel sintering plant 180m 2 The SCR denitration reactor of the sintering machine is provided with a CO energy-saving emission-reducing pipeline, CO in sintering flue gas is catalytically combusted and reused, and before the CO energy-saving emission-reducing pipeline is applied, the discharged waste gas of the sintering machine of the plant contains 6000-12000mg/Nm 3 After the CO energy-saving emission-reducing pipeline of the embodiment is applied, the CO content in the discharged sintering flue gas is only 2000-4500mg/Nm through on-site primary measurement 3 The CO content in the sintering flue gas emission is reduced by 60-70%, and meanwhile, the combustion heat passes through the GGH heat exchanger to heat and improve the sintering initial flue gas temperature by more than 30 ℃, so that the blast furnace gas consumption of the hot blast furnace burner of the original denitration system can be greatly reduced.
The above disclosure is intended only to illustrate one or more preferred embodiments of the present invention and not to limit the invention in any way, which is intended to be encompassed by the present invention.
Claims (9)
1. The utility model provides a reduce reaction unit of CO emission in flue gas, includes SCR reaction tower and GGH heat exchanger that is used for sintering flue gas denitration to handle which characterized in that: the system also comprises a CO energy-saving emission-reducing pipeline;
the CO energy-saving emission-reducing pipeline is sequentially connected with a first heat exchange side of the GGH heat exchanger, a combustion catalyst, a second heat exchange side of the GGH heat exchanger and a flue gas output pipeline through a sintering flue gas input pipeline;
the combustion catalyst is arranged in the SCR reaction tower, and is filled with palladium catalyst so that the palladium catalyst catalyzes CO to generate combustion reaction at the temperature of 250-300 ℃ when the sintering flue gas of the CO energy-saving emission-reducing pipeline passes through the combustion catalyst, the CO combustion of the sintering flue gas improves the flue gas temperature in the SCR reaction tower, and the high-temperature flue gas enters the second heat exchange side of the GGH heat exchanger so that the sintering flue gas at the first heat exchange side of the GGH heat exchanger has high flue gas temperature before entering the SCR reaction tower.
2. The reaction equipment for reducing the emission of CO in flue gas according to claim 1, wherein: and a direct combustion device is arranged between the first heat exchange side of the GGH heat exchanger of the CO energy-saving emission-reducing pipeline and the SCR reaction tower, and is provided with a temperature sensor at a flue gas inlet of the SCR reaction tower and the first heat exchange side of the GGH heat exchanger for monitoring the sintering flue gas temperature before entering the SCR reaction tower.
3. The reaction equipment for reducing the emission of CO in flue gas according to claim 1, wherein: the temperature of the sintering flue gas in the SCR reaction tower for carrying out normal nitrogen oxide catalytic reaction is 280-300 ℃.
4. The reaction equipment for reducing the emission of CO in flue gas according to claim 3, wherein: and after the flue gas enters the second heat exchange side of the GGH heat exchanger, the CO combustion of the sintering flue gas raises the heat exchange temperature of the first heat exchange side of the GGH heat exchanger by more than 30 ℃ so as to raise the temperature of the combustion flue gas passing through the first heat exchange side of the GGH heat exchanger to 280 ℃.
5. The reaction equipment for reducing the emission of CO in flue gas according to claim 1, wherein: the combustion catalyst is coated with palladium catalysts, the palladium catalysts at least comprise catalytic activity coatings and palladium metal coatings, the catalytic activity coatings are coated on the walls of the flow channels of the combustion catalyst, the palladium metal coatings are formed by coating palladium metal liquid on the catalytic activity coatings and drying the palladium metal liquid, and the catalytic activity coatings respectively comprise active oxides catalytically activated by palladium.
6. An energy-saving emission-reducing method for reducing the emission of CO in flue gas is characterized by comprising the following steps:
sintering flue gas enters a first heat exchange side of the GGH heat exchanger from a sintering flue gas input pipeline to perform heat exchange and raise the temperature to a reaction temperature;
catalyzing CO by a palladium catalyst at a reaction temperature state to perform a combustion reaction when sintering flue gas in the SCR reaction tower passes through a combustion catalyst;
the heat released by CO combustion reaction is used for increasing the temperature of the flue gas in the SCR reaction tower, and the high-temperature flue gas exchanges heat with the sintering flue gas at the first heat exchange side of the GGH heat exchanger when passing through the second heat exchange side of the GGH heat exchanger, so that the temperature of the sintering flue gas can be increased to the reaction temperature required by SCR denitration reaction;
the high-temperature flue gas is discharged from the flue gas output pipeline after being subjected to catalytic combustion and combustion heat exchange of the CO energy-saving emission-reducing pipeline, and the CO content in the discharged flue gas is reduced by 60-70%.
7. The energy-saving emission-reducing method for reducing the emission of CO in the flue gas according to claim 6, further comprising the following steps:
a direct combustion device is arranged between a first heat exchange side of a GGH heat exchanger of the CO energy-saving emission-reducing pipeline and the SCR reaction tower;
monitoring the reaction temperature before the sintering flue gas enters the SCR reaction tower and the heat exchange temperature of the first heat exchange side of the GGH heat exchanger, and comparing:
when the heat exchange temperature is lower than the reaction temperature, starting the direct combustion device to heat the sintering flue gas flowing through to the reaction temperature;
when the heat exchange temperature is equal to or higher than the reaction temperature, the direct-combustion device is stopped to save energy.
8. The energy-saving emission-reducing method for reducing the emission of CO in flue gas according to claim 6, characterized in that: the palladium catalyst catalyzes CO to carry out combustion reaction at the reaction temperature of 250-300 ℃.
9. The energy-saving emission-reducing method for reducing the emission of CO in flue gas according to claim 6, characterized in that: when the high-temperature flue gas passes through the second heat exchange side of the GGH heat exchanger, the high-temperature flue gas exchanges heat with the low-temperature sintering flue gas at the first heat exchange side of the GGH heat exchanger to increase the heat exchange temperature by more than 30 ℃, and the original heat exchange temperature at the first heat exchange side of the GGH heat exchanger is increased to 280 ℃ required by SCR denitration reaction from 250 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116447886A (en) * | 2023-04-24 | 2023-07-18 | 北京皓天百能环保工程有限公司 | Method for utilizing combustible CO in sintering flue gas through catalytic combustion |
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2022
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116447886A (en) * | 2023-04-24 | 2023-07-18 | 北京皓天百能环保工程有限公司 | Method for utilizing combustible CO in sintering flue gas through catalytic combustion |
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