CN117839428A - Energy-saving flue gas denitration system - Google Patents
Energy-saving flue gas denitration system Download PDFInfo
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- CN117839428A CN117839428A CN202410263094.5A CN202410263094A CN117839428A CN 117839428 A CN117839428 A CN 117839428A CN 202410263094 A CN202410263094 A CN 202410263094A CN 117839428 A CN117839428 A CN 117839428A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 239000003546 flue gas Substances 0.000 title claims abstract description 189
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- 238000010438 heat treatment Methods 0.000 claims abstract description 31
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 27
- 230000003197 catalytic effect Effects 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 21
- 230000003647 oxidation Effects 0.000 claims abstract description 20
- 239000002737 fuel gas Substances 0.000 claims abstract description 19
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 13
- 238000002485 combustion reaction Methods 0.000 claims description 19
- 239000000463 material Substances 0.000 claims description 11
- 230000007246 mechanism Effects 0.000 claims description 11
- 239000013543 active substance Substances 0.000 claims description 8
- 238000002347 injection Methods 0.000 claims description 6
- 239000007924 injection Substances 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims 3
- 238000005507 spraying Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000010531 catalytic reduction reaction Methods 0.000 abstract 1
- 239000010410 layer Substances 0.000 description 35
- 238000005245 sintering Methods 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 239000011149 active material Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002356 single layer Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000006557 surface reaction Methods 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/864—Removing carbon monoxide or hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/869—Multiple step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/502—Carbon monoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention provides an energy-saving flue gas denitration system, which relates to the technical field of energy conservation and environmental protection, and comprises a flue, wherein one end of the flue is provided with a flue inlet, the other end of the flue is provided with a flue outlet, the direction of the flue inlet is sequentially provided with a turbulent flow grid, a built-in heating furnace for burning CO in flue gas, a CO catalytic oxidation layer and an ammonia spraying grid, the direction of the flue outlet is provided with an SCR (selective catalytic reduction) reactor filled with a catalyst, and the flue inlet and the flue outlet are provided with rotary flue gas heat exchangersIs CO 2 The heat is released, so that the temperature of the flue gas is increased, and the fuel gas consumption required for heating the flue gas can be reduced.
Description
Technical Field
The invention relates to the technical field of energy conservation and environmental protection, in particular to an energy-saving flue gas denitration system.
Background
The concentration of nitrogen oxides in the sintering flue gas is 250-350 mg/Nm3, the emission standard of nitrogen oxides is required to be 50mg/Nm3 in the opinion of ultra-low emission, and the requirements of places are more stringent to be 35mg/Nm3. The environmental protection tax law lists CO in the flue gas as an object for tax collection of atmospheric pollutants, and the equivalent value is 16.7, which is inferior to styrene and carbon disulfide, and the third rank among 44 tax-applicable atmospheric pollutants becomes a key point in the treatment of the atmospheric pollutants.
For a denitration efficiency of approximately 90%, the sintering flue gas does not have a high Wen Tuoxiao section, and the SNCR denitration and the pre-SCR denitration (that is, SCR denitration is before and desulfurization is after) cannot be adopted. The existing sintering flue gas denitration systems all adopt post SCR denitration, namely sintering flue gas is firstly desulfurized and then denitrated, and the denitration temperature is 200-300 ℃. However, the temperature after desulfurization does not exceed 85 ℃ in the desulfurization process before denitration, whether the desulfurization process is a semi-dry process or a wet process, so that the flue gas needs to be heated in order to obtain a proper denitration temperature.
The heating furnace needs to burn the blast furnace fuel gas rich in CO, and each ton of sintered ore needs 16-18kg CO, namely 50m 3 The left and right blast furnace fuel gas, the sintering flue gas contains CO with the concentration of 6000-8000 mg/Nm3, the CO discharged along with the flue gas is 18-25 kg/ton of sintered ore, and the consumed CO-rich blast furnace fuel gas and the sintering flue gas discharge high-concentration CO per se to form clear technical contradiction.
Therefore, how to utilize the chemical energy of CO in the flue gas to heat the flue gas, so as to reduce the consumption of the blast furnace fuel gas and reduce the CO concentration discharged in the sintering flue gas is a technical problem to be solved urgently by those skilled in the art.
Disclosure of Invention
Accordingly, the present invention aims to provide an energy-saving flue gas denitration system, which solves the technical problems of high fuel gas consumption and high concentration of CO discharged from sintering flue gas caused by the lack of an effective way for heating desulfurized flue gas in the prior art
In order to achieve the above purpose, the invention provides an energy-saving flue gas denitration system, which comprises a flue for circulating flue gas, wherein one end of the flue is provided with a flue gas inlet, the other end of the flue is provided with a flue gas outlet, a turbulent flow grid, a built-in heating furnace for burning CO in flue gas, a CO catalytic oxidation layer and an ammonia spraying grid are sequentially arranged in the direction of the flue gas inlet, an SCR reactor filled with a catalyst is arranged in the direction of the flue gas outlet, a rotary flue gas heat exchanger is arranged at the flue gas inlet and the flue gas outlet, and hot flue gas after denitration is heated by using cold flue gas before denitration by the rotary flue gas heat exchanger.
Optionally, the flue is 180-degree bent.
Optionally, the diameter of the flue in the direction of the flue outlet is larger than the diameter of the flue in the direction of the flue inlet.
Optionally, the rotary flue gas heat exchanger comprises a shell, a rotor and a heat exchange element, wherein the shell is connected with the flue and is divided into a raw flue gas inlet, a raw flue gas outlet, a clean flue gas inlet and a clean flue gas outlet, the rotor is rotatably arranged on the shell and is a compartment formed by a circumferential partition plate and a radial partition plate, and the heat exchange element is positioned in the compartment.
Optionally, the raw flue gas inlet and the raw flue gas outlet are oppositely arranged and positioned in the direction of the flue gas inlet; the clean flue gas inlet and the clean flue gas outlet are arranged in pairs and positioned in the direction of the flue gas outlet.
Optionally, the rotary flue gas heat exchanger further comprises a driving mechanism and a bearing, wherein the bearing is arranged at the end part of the rotor, the driving mechanism is in driving connection with the rotor, and the driving mechanism drives the rotor to rotate around the bearing.
Optionally, the built-in heating furnace is the combustor, the combustor is by the casing with arrange in the inside some firearm of casing constitutes, be equipped with fuel gas interface, combustion-supporting wind interface, with flange and steady combustion cylinder that the flue is connected on the casing, fuel gas interface and fuel gas valves switch on, combustion-supporting wind interface and combustion-supporting wind valves switch on, combustion-supporting wind valves connects the combustion-supporting fan.
Optionally, the internal heating furnace, flame combustion occurs in the flue, and a part of CO in the flue gas can be combusted.
Optionally, the CO catalytic oxidation layer includes at least one layer, is disposed on the inner wall of the flue, and is installed downstream of the built-in heating furnace, upstream of the ammonia injection grid, and the catalyst of the CO catalytic oxidation layer is in a honeycomb structure and is composed of a base material and an active substance.
Optionally, the SCR reactor includes a middle-low temperature denitration catalyst layer, where the middle-low temperature denitration catalyst layer includes at least one layer, and is disposed on an inner wall of the flue, and a catalyst of the middle-low temperature denitration catalyst layer is in a honeycomb structure and is composed of a base material and an active material.
The energy-saving flue gas denitration system provided by the invention has the following technical effects:
the energy-saving flue gas denitration system comprises a flue, wherein one end of the flue is provided with a flue gas inlet, the other end of the flue is provided with a flue gas outlet, the flue gas inlet direction is sequentially provided with a turbulent flow grid, a built-in heating furnace for burning CO in flue gas, a CO catalytic oxidation layer and an ammonia spraying grid, the flue gas outlet direction is provided with an SCR reactor filled with a catalyst, the flue gas inlet and the flue gas outlet are provided with rotary flue gas heat exchangers, the rotary flue gas heat exchangers use hot flue gas after denitration to heat cold flue gas before denitration, and the concentration of CO discharged in sintering flue gas can be reduced by arranging the built-in heating furnace and the CO catalytic oxidation layer, and CO in flue gas is converted into CO 2 The heat is released, so that the temperature of the flue gas is increased, and the fuel gas consumption required for heating the flue gas can be reduced.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a preferred embodiment of an energy-efficient flue gas denitration system according to the present invention;
FIG. 2 is a side view of the energy efficient flue gas denitration system of FIG. 1;
FIG. 3 is a schematic diagram of a rotary flue gas heat exchanger of the energy-saving flue gas denitration system in FIG. 1;
fig. 4 is a schematic structural diagram of a built-in heating furnace of the energy-saving flue gas denitration system in fig. 1.
Wherein, fig. 1-4:
1. a flue; 11. a flue gas inlet; 12. a flue gas outlet;
2. a spoiler grid;
3. a built-in heating furnace; 31. a burner; 311. a fuel gas interface; 312. a combustion-supporting air interface; 32. a flange; 33. a stable combustion cylinder;
4. a CO catalytic oxidation layer;
5. an ammonia spraying grid;
6. a medium-low temperature denitration catalyst layer;
7. a rotary flue gas heat exchanger; 71. a housing; 72. a rotor; 721. a compartment; 73. a driving mechanism; 74. and (3) a bearing.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It will be apparent that the described embodiments are only some, but not all, embodiments of the invention. All other embodiments, based on the examples herein, which are within the scope of the invention as defined by the claims, will be within the scope of the invention as defined by the claims.
As shown in fig. 1-4, the structure or a part of the structure of a preferred embodiment of the energy-saving flue gas denitration system of the present invention is schematically shown, and the energy-saving flue gas denitration system includes a flue 1, where the flue 1 is mainly used for realizing the circulation of flue gas.
As shown in fig. 1, the flue 1 in this embodiment is bent at 180 degrees, one end of the flue is a flue gas inlet 11, the other end of the flue is a flue gas outlet 12, the flue gas inlet 11 is low-temperature non-denitration flue gas, and the flue gas outlet 12 is high-temperature denitration flue gas.
With continued reference to fig. 1, the flue gas inlet 11 is provided with a turbulent flow grid 2, a built-in heating furnace 3 for burning CO in the flue gas, a CO catalytic oxidation layer 4 and an ammonia injection grid 5 in sequence.
The turbulent flow grid 2 is arranged in the flue 1, and can form vortex for flue gas, so that the flue gas contacted with combustion flame of the hot blast stove is in a vortex state and better participates in combustion, and the structure is common in the prior art, and the invention is not repeated.
As shown in fig. 4, the built-in heating furnace 3 for burning CO in flue gas is a burner 31, the burner 31 is composed of a shell and an igniter arranged in the shell, a fuel gas interface 311, a flange 32 connected with a flue 1 and a stable combustion cylinder 33 are arranged on the shell, the fuel gas interface 311 is communicated with a fuel gas valve group, the stable combustion cylinder 33 penetrating into the flue 1 is not more than 2m, when the flue gas negative pressure at the built-in heating furnace 3 is more than 3kpa, the supply of combustion-supporting air can be satisfied, a combustion-supporting fan is not required to be arranged, the air combustion-supporting form without the fan is adopted, and the electricity consumption of the fan in operation is saved.
When the negative pressure of the flue 1 can not meet the supply of combustion supporting air, the shell is also provided with a supporting air interface 312, the supporting air interface 312 is communicated with a supporting air valve group, the supporting air valve group is connected with a supporting air blower, namely, the negative pressure of the flue 1 is realized through the supporting air blower, the flue gas of the flue 1 is not used as the supporting air of the built-in heating furnace 3, and the service life of the igniter and the running stability and safety of the heating furnace are ensured.
The energy-saving flue gas denitration system of the embodiment adopts the built-in heating furnace 3, flame combustion occurs in the flue 1, and part of CO in the flue gas can be combusted, so that the concentration of CO is reduced, the load of a subsequent catalytic oxidation layer is reduced, and the installation quantity of a catalyst is reduced.
The CO catalytic oxidation layer 4 of the present embodiment includes at least one layer, and is disposed on the inner wall of the flue 1, and the catalyst of the CO catalytic oxidation layer 4 has a honeycomb structure and is composed of a base material and an active material.
The CO catalytic oxidation layer 4 is a catalyst-mounting bed layer, which is placed downstream of the built-in heating furnace 3, upstream of the ammonia injection grid 5, and may be a single layer or a plurality of layers depending on the amount of CO to be removed. The CO catalyst is in a honeycomb structure and consists of a base material and an active substance, and the base material and the active substance of the catalyst with different functions are different. The catalyst is integrally formed, the smallest unit is square, the size is 150mm multiplied by 150mm, each module contains a plurality of units, and each module contains a certain proportion of test blocks. The number of pores of the honeycomb catalyst is determined by the concentration of particles in the flue gas and the catalytic performance, and the catalyst applied to the sintering flue gas is generally 25 pores or 30 pores.
The energy-saving flue gas denitration system of the embodiment has two purposes: 1. reducing the concentration of CO discharged in sintering flue gas; 2. the fuel gas consumption of the sintering flue gas denitration system is reduced, and the two purposes complement each other. Mainly due to CO and O 2 The reaction is a strongly exothermic reaction, i.e., CO+Layer O 2 →CO 2 ，∆H=267 kJ/mol。
The reduction of the concentration of CO emitted in the sintering flue gas is mainly achieved by two steps:
the first step, the combustion of the built-in heating furnace 3 occurs in the flue 1, and the burning flame can burn the residual CO in the sintering flue gas;
in the second step, the flue gas undergoes CO catalytic oxidation through the CO catalytic oxidation layer 4 to perform gas-solid surface reaction, wherein the reaction process is as follows: diffusion, adsorption, reaction, desorption and diffusion, namely CO and O in the flue gas 2 The molecules diffuse to the surface of the catalyst, and the noble metal active sites adsorbed to the catalyst react to generate CO 2 The molecules are diffused into the flue gas after desorption.
Through two-step reaction, CO in the flue gas is converted into CO 2 And the heat is released, so that the temperature of the flue gas is increased, and the fuel gas consumption required for heating the flue gas can be reduced.
With continued reference to fig. 1 and 2, the ammonia injection grid 5 is located downstream of the CO catalytic oxidation layer 4, and ammonia injected into the flue 1 does not pass through the CO catalytic oxidation layer 4, so that oxidation reaction does not occur, and ammonia consumption is only that of denitration reaction.
With continued reference to fig. 1, the direction of the flue gas outlet 12 is provided with an SCR reactor filled with a catalyst, the SCR reactor comprises a middle-low temperature denitration catalyst layer 6, the middle-low temperature denitration catalyst layer 6 comprises at least one layer, the catalyst of the middle-low temperature denitration catalyst layer 6 is in a honeycomb structure and consists of a base material and an active substance, and the catalyst is arranged on the inner wall of the flue 1.
The middle-low temperature denitration catalyst layer 6 is a bed layer provided with a catalyst, the amount of NOx to be removed can be single-layer or multi-layer according to the requirement, and the denitration catalyst is in a honeycomb structure and consists of a base material and an active substance. The catalyst base materials and active substances with different functions are different, the catalyst is integrally formed, the smallest unit is square, the size is 150mm multiplied by 150mm, each module contains a plurality of units, and each module contains a certain proportion of test blocks. The number of pores of the honeycomb catalyst is determined by the concentration of particles in the flue gas and the catalytic performance, and the catalyst applied to the sintering flue gas is generally 25 pores or 30 pores. The using temperature of the medium-low temperature denitration catalyst is 180-220 ℃.
In addition, the diameter of the flue 1 in the direction of the flue gas outlet 12 is larger than that of the flue 1 in the direction of the flue gas inlet 11, the rotary flue gas heat exchanger 7 is arranged at the positions of the flue gas inlet 11 and the flue gas outlet 12, and the rotary flue gas heat exchanger 7 heats the hot flue gas after denitration by using the cold flue gas before denitration.
Specifically, as shown in fig. 3, the rotary flue gas heat exchanger 7 includes a housing 71, a rotor 72 and a heat exchange element, the housing 71 is connected with the flue 1 and is divided into a raw flue gas inlet 11, a raw flue gas outlet 12, a clean flue gas inlet 11 and a clean flue gas outlet 12, the raw flue gas inlet 11 and the raw flue gas outlet 12 are oppositely arranged and are positioned in the direction of the flue gas inlet 11, and the clean flue gas inlet 11 and the clean flue gas outlet 12 are arranged in pairs and are positioned in the direction of the flue gas outlet 12; the rotor 72 is rotatably arranged on the housing 71 and is a compartment 721 formed by circumferential and radial partitions, and the heat exchanging elements are located within the compartment 721.
The rotary flue gas heat exchanger 7 further comprises a driving mechanism 73 and a bearing 74, the bearing 74 is arranged at the end part of the rotor 72, the driving mechanism 73 is in driving connection with the rotor 72, and the driving mechanism 73 drives the rotor 72 to rotate around the bearing 74.
The heat exchange element is arranged in two layers, the upper layer (hot end) is made of special wave type Cooden steel, and the lower layer (cold end) is made of special wave type enamel plating material, so that the acid dew point corrosion protection and the ammonium bisulfate deposition corrosion protection can be considered.
The rotary flue gas heat exchanger 7 heats the cold raw flue gas before denitration by using the hot clean flue gas after denitration, and the flue gas is self-heated by a heat exchange element arranged in the heat exchanger body. The rotor 72 rotates under the drive of the drive mechanism 73, the heat exchange element contacts with the hot clean flue gas, the heat in the flue gas is absorbed, the heat exchange element absorbing the heat rotates to the side of the raw flue gas, the heat is released to the cold raw flue gas, the heat exchange element continuously absorbs and releases the heat, and the self-heating of the flue gas is completed.
The specific process of the energy-saving flue gas denitration system in the embodiment is as follows:
(1) The flue gas after desulfurization and dust removal firstly enters the cold end of the original flue gas side of the rotary flue gas heat exchanger 7 through the flue 1, and flows out from the hot end of the original flue gas side after being heated by the heat exchange element;
(2) The flue gas forms vortex through a vortex grid 2 arranged in the flue 1;
(3) Through a built-in heating furnace 3 which is partially arranged in the flue 1, the heating furnace is involved in combustion and is mixed with hot air generated by the combustion;
(4) The flue gas after heating is reacted by the CO catalytic oxidation layer 4 to generate CO 2 And release heat, the flue gas temperature is further raised;
(5) After reaching the denitration reaction temperature, the wastewater passes through an ammonia injection grid 5 arranged in the flue 1;
(6) The flue gas and ammonia gas are mixed and then reach a middle-low temperature denitration catalyst layer 6 in the SCR reactor to carry out denitration reaction;
(7) The flue gas after denitration enters the hot end of the flue gas purifying side of the rotary flue gas heat exchanger 7, heat in the flue gas is transferred to the heat exchange element, and the flue gas flows into the next flue gas device from the cold end of the flue gas purifying side after being cooled, so that denitration is completed.
In the description of the present invention, it is to be noted that, unless otherwise indicated, the meaning of "plurality" means two or more; the terms "upper," "lower," "left," "right," "inner," "outer," "front," "rear," "head," "tail," and the like are used as an orientation or positional relationship based on that shown in the drawings, merely to facilitate description of the invention and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the invention. Furthermore, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the above terms in the present invention can be understood as appropriate by those of ordinary skill in the art.
The foregoing is merely illustrative of the present invention, and the present invention is not limited thereto, and any person skilled in the art will readily recognize that variations or substitutions are within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. The utility model provides an energy-conserving flue gas denitration system, its characterized in that, including the flue that is used for making the flue gas circulate, the one end of flue is equipped with the flue gas import, the other end of flue is equipped with the flue gas export, flue gas import direction is equipped with vortex grid, the built-in heating furnace of CO in the burning flue gas, CO catalytic oxidation layer and spouts the ammonia grid in proper order, flue gas export direction department is equipped with the SCR reactor that loads the catalyst, the flue gas import with flue gas export department is equipped with rotary flue gas heat exchanger, the hot flue gas after the rotary flue gas heat exchanger uses the denitration is the cold flue gas heating before the denitration.
2. The energy efficient flue gas denitration system of claim 1, wherein the flue is 180 degree bent.
3. The energy efficient flue gas denitration system of claim 1, wherein the diameter of the flue in the direction of the flue gas outlet is greater than the diameter of the flue in the direction of the flue gas inlet.
4. The energy efficient flue gas denitration system according to claim 1, wherein the rotary flue gas heat exchanger comprises a housing, a rotor and a heat exchange element, the housing is connected with the flue and is divided into a raw flue gas inlet, a raw flue gas outlet, a clean flue gas inlet and a clean flue gas outlet, the rotor is rotatably arranged on the housing and is a compartment formed by a circumferential partition plate and a radial partition plate, and the heat exchange element is positioned in the compartment.
5. The energy-saving flue gas denitration system according to claim 4, wherein the raw flue gas inlet and the raw flue gas outlet are arranged opposite to each other and positioned in the flue gas inlet direction; the clean flue gas inlet and the clean flue gas outlet are arranged in pairs and positioned in the direction of the flue gas outlet.
6. The energy-saving flue gas denitration system according to claim 4, wherein the rotary flue gas heat exchanger further comprises a driving mechanism and a bearing, the bearing is arranged at the end part of the rotor, the driving mechanism is in driving connection with the rotor, and the driving mechanism drives the rotor to rotate around the bearing.
7. The energy-saving flue gas denitration system according to claim 1, wherein the built-in heating furnace is a burner, the burner is composed of a shell and an igniter arranged in the shell, a fuel gas interface, a combustion air interface, a flange connected with the flue and a stable combustion cylinder are arranged on the shell, the fuel gas interface is communicated with a fuel gas valve bank, the combustion air interface is communicated with a combustion air valve bank, and the combustion air valve bank is connected with a combustion fan.
8. The energy efficient flue gas denitration system of claim 1, wherein the internal heating furnace is configured such that flame combustion occurs in the flue and a portion of the CO in the flue gas can be combusted.
9. The energy-saving flue gas denitration system according to claim 1, wherein the CO catalytic oxidation layer comprises at least one layer, is arranged on the inner wall of the flue and is arranged at the downstream of the built-in heating furnace and at the upstream of the ammonia injection grid, and the catalyst of the CO catalytic oxidation layer is in a honeycomb structure and consists of a base material and an active substance.
10. The energy-saving flue gas denitration system according to claim 1, wherein the SCR reactor comprises a middle-low temperature denitration catalyst layer, the middle-low temperature denitration catalyst layer comprises at least one layer, the middle-low temperature denitration catalyst layer is arranged on the inner wall of the flue, and the catalyst of the middle-low temperature denitration catalyst layer is in a honeycomb structure and consists of a base material and an active substance.
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