CN108176221B - Sintering flue gas temperature rising denitration device and sintering flue gas temperature rising denitration method - Google Patents
Sintering flue gas temperature rising denitration device and sintering flue gas temperature rising denitration method Download PDFInfo
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- CN108176221B CN108176221B CN201711460887.2A CN201711460887A CN108176221B CN 108176221 B CN108176221 B CN 108176221B CN 201711460887 A CN201711460887 A CN 201711460887A CN 108176221 B CN108176221 B CN 108176221B
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- 239000003546 flue gas Substances 0.000 title claims abstract description 168
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 158
- 238000005245 sintering Methods 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 28
- 230000000630 rising effect Effects 0.000 title claims abstract description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 67
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 40
- 230000023556 desulfurization Effects 0.000 claims abstract description 40
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 24
- 239000000428 dust Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 18
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 12
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 239000003054 catalyst Substances 0.000 claims description 19
- 238000002485 combustion reaction Methods 0.000 claims description 11
- 238000010790 dilution Methods 0.000 claims description 5
- 239000012895 dilution Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 abstract description 20
- 238000004064 recycling Methods 0.000 abstract description 7
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000002440 industrial waste Substances 0.000 abstract description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 15
- 230000009467 reduction Effects 0.000 description 11
- 230000000694 effects Effects 0.000 description 10
- 238000004134 energy conservation Methods 0.000 description 10
- 238000005507 spraying Methods 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000009766 low-temperature sintering Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
- F23L15/04—Arrangements of recuperators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Sintering flue gas temperature rising denitration equipment and sintering flue gas temperature rising denitration method belong to the field of industrial waste gas treatment. The sintering flue gas temperature rising denitration device comprises a denitration tower, and an air inlet flue and an exhaust flue which are connected with the denitration tower, wherein the air inlet flue is connected with an ammonia conveying pipe and a flue burner, a flue gas-flue gas reheater for heat exchange is connected between the air inlet flue and the exhaust flue, the exhaust flue is connected with a desulfurization tower, and the top of the desulfurization tower is provided with a wet-type electric dust collector. The device can effectively recycle waste heat by adopting an energy two-stage recycling method. The sintering flue gas temperature rise denitration method comprises the following steps: heating sintering flue gas to 300-320 ℃, mixing the sintering flue gas with ammonia gas, and carrying out catalytic reaction to obtain denitration clean flue gas; and heat exchange cooling the denitration purified flue gas and the sintering flue gas before heating to 150-160 ℃ and then desulfurizing and dedusting. The method can recover waste heat by adopting an energy two-stage recovery and utilization method so as to save energy.
Description
Technical Field
The invention relates to the field of industrial waste gas treatment, in particular to sintering flue gas temperature rising denitration equipment and a sintering flue gas temperature rising denitration method.
Background
The sintering machine in the iron and steel plant has great smoke discharge amount and great pollution to the environment, and the main pollutant in the smoke discharged by the sintering machine is NO X 、SO 2 And dust. Therefore, the sintering plant flue gas must be subjected to flue gas desulfurization and denitrification treatment to reduce pollution.
Because the temperature of sintering flue gas is lower, at present, the sintering machine in China generally adopts wet desulfurization, a denitration device is not arranged, white smoke is easy to appear at a chimney outlet, and most of sintering factories in China need denitration reconstruction treatment aiming at environmental protection requirements. At present, the domestic sintering flue gas denitration technology is mainly divided into three types: activated carbon method, SCR denitration and ozone oxidation denitration. The active carbon method is an integrated technology of desulfurization and denitrification, and is suitable for purifying the flue gas of a newly-built sintering machine. Ozone oxidation denitration technology is suitable for NO X Low concentration flue gas, high concentration NO X The flue gas adopts ozone oxidation denitration to ensure denitration efficiency difficultly, and the running cost is too high. The SCR denitration technology takes ammonia as a reducing agent, and utilizes a catalyst to remove NO in a temperature range of 280-420 DEG C X Reduction to N 2 The denitration technology is mature and has high denitration efficiency. Because the temperature of the sintering flue gas is lower, the sintering flue gas needs to be heated for ensuring the denitration effect and the normal operation of the system, the residual heat utilization rate of the traditional temperature-rising SCR denitration process is low, the operation cost is higher, and the requirements of energy conservation and emission reduction of the existing steel mill cannot be met.
Therefore, a sintering flue gas denitration method and equipment capable of improving the utilization rate of waste heat to save energy and reduce emission are needed.
Disclosure of Invention
The invention aims to provide sintering flue gas temperature rising denitration equipment which can effectively utilize waste heat for preheating and has the effects of high efficiency, energy conservation and waste gas emission reduction by two-stage recycling of the waste heat.
The invention further aims to provide a sintering flue gas temperature rising denitration method which can utilize waste heat to perform two-stage recycling so as to achieve the effects of energy conservation and emission reduction.
Embodiments of the present invention are implemented as follows:
a sintering flue gas temperature rising denitration method comprises the following steps:
heating sintering flue gas to 300-320 ℃, mixing the sintering flue gas with ammonia gas, introducing the mixture to the surface of a denitration catalyst, and carrying out catalytic reaction to obtain denitration clean flue gas;
and carrying out heat exchange cooling on the denitration purified flue gas and the sintering flue gas before heating to 150-160 ℃, and then carrying out desulfurization and dust removal treatment to obtain discharged flue gas.
In the preferred embodiment of the invention, the denitration flue gas is subjected to heat exchange with the sintering flue gas before heating, so that the sintering flue gas is heated to 250-260 ℃ and the denitration flue gas is cooled to 160-170 ℃.
In the preferred embodiment of the invention, the combustion air is subjected to heat exchange with the denitration clean flue gas cooled to 160-170 ℃ so that the combustion air is heated to 130-140 ℃ and then is used for heating the sintering flue gas, and the denitration clean flue gas is cooled to 150-160 ℃.
In the preferred embodiment of the invention, the flue gas after the wet flue gas is heated to 200-210 ℃ and then mixed with the flue gas after the wet electric dust removal treatment, and the flue gas after the catalytic reaction is cooled to 290-300 ℃ and then exchanges heat with the sintering flue gas before the heating.
In a preferred embodiment of the invention, the ammonia gas is mixed with the additional sintering flue gas and then mixed with the sintering flue gas heated to 300-320 ℃ and introduced to the surface of the catalyst.
In a preferred embodiment of the present invention, the above-mentioned NO in the exhaust fumes X The content is 100mg/Nm 3 The denitration efficiency is more than 90%, SO 2 The content is 30mg/Nm 3 The dust concentration was below 10mg/Nm 3 The following is given.
The utility model provides a sintering flue gas intensification denitration device, its includes denitration tower and the flue and the exhaust flue of admitting air that are connected with the denitration tower, and the flue that admit air is connected with ammonia conveyer pipe and is used for flowing through the flue combustor of flue heating to admitting air in the flue, is connected with the flue gas-flue gas reheater that is used for heat transfer between admitting air flue and the exhaust flue, and the exhaust flue is connected with the desulfurizing tower, and the top of desulfurizing tower is equipped with wet-type electrostatic precipitator.
In a preferred embodiment of the present invention, the exhaust flue is provided with a primary air preheater, and a first air inlet and a first air outlet of the primary air preheater are respectively connected with a combustion-supporting fan and a flue burner.
In a preferred embodiment of the invention, the exhaust flue is further provided with a secondary air preheater, a second air inlet and a second air outlet of the primary air preheater are respectively connected with a desulfurization chimney white air removal fan and an air inlet of the secondary air preheater, and an air outlet of the secondary air preheater is communicated with the top of the desulfurization tower.
In the preferred embodiment of the invention, the ammonia gas conveying pipe is connected with a mixer, the mixer is connected with a high-temperature dilution fan and an ammonia gas evaporator, and an inlet and an outlet of the ammonia gas evaporator are respectively connected with an ammonia water tank and a desulfurizing tower.
The embodiment of the invention has the beneficial effects that: the sintering flue gas temperature rising denitration device provided by the embodiment of the invention comprises a denitration tower, an air inlet flue and an exhaust flue, wherein the air inlet flue and the exhaust flue are connected with the denitration tower, the air inlet flue is connected with an ammonia conveying pipe and a flue burner for heating flue gas flowing through the air inlet flue, a flue gas-flue gas reheater for heat exchange is connected between the air inlet flue and the exhaust flue, the exhaust flue is connected with a desulfurization tower, and the top of the desulfurization tower is provided with a wet electric dust collector. The sintering flue gas temperature rising denitration device can effectively utilize waste heat for preheating, and adopts the two-stage waste heat recovery device to exchange heat between different temperature ranges for a plurality of times, so that the energy contained in the discharged high Wen Tuoxiao flue gas is recovered and efficiently utilized in multiple stages, and the effects of energy conservation and emission reduction are achieved. The sintering flue gas temperature rise denitration method comprises the following steps: heating sintering flue gas to 300-320 ℃, mixing the sintering flue gas with ammonia gas, introducing the mixture to the surface of a denitration catalyst, and carrying out catalytic reaction to obtain denitration clean flue gas; and carrying out heat exchange cooling on the denitration purified flue gas and the sintering flue gas before heating to 150-160 ℃, and then carrying out desulfurization and dust removal treatment to obtain discharged flue gas. According to the sintering flue gas temperature rising denitration method, two-stage energy recovery can be adopted to recycle energy in denitration flue gas for multiple times in stages, so that the recycling rate of waste heat is effectively improved, and the effects of energy conservation and emission reduction are achieved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a sintering flue gas temperature-rising denitration device provided in embodiment 1 of the present invention;
FIG. 2 is a schematic view of the structure of the ammonia injection grid of the present invention;
FIG. 3 is a schematic view of a first pressure reducing plate according to the present invention;
fig. 4 is a schematic structural diagram of a sintering flue gas temperature-rising denitration system provided in embodiment 2 of the present invention.
In the figure: 001-sintering flue gas temperature rise denitration equipment; a 100-denitration tower; 101-a denitration catalyst; 110-an air inlet flue; 120-exhaust flue; 130-ammonia gas delivery pipe; 140-flue burner; 150-a flue gas-flue gas reheater; 160-desulfurizing tower; 170-wet electric dust collector; 180-primary air preheater; 190-combustion-supporting fans; 200-a secondary air preheater; 210-a white gas eliminating fan of a desulfurization chimney; 220-a mixer; 230-a high-temperature dilution blower; 240-ammonia evaporator; 250-ammonia water tank; 260-ammonia injection grid; 261-ammonia spraying pipe; 262-ammonia spraying holes; 270-a wastewater tank; 280-a first pressure relief panel; 290-a second pressure relief panel; 300-a third pressure reducing plate.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further definition or explanation thereof is necessary in the following figures.
In the description of the present invention, it should be noted that, directions or positional relationships indicated by terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., are directions or positional relationships based on those shown in the drawings, or are directions or positional relationships conventionally put in use of the inventive product, are merely for convenience of describing the present invention and simplifying the description, and are not indicative or implying that the apparatus or element to be referred to must have a specific direction, be constructed and operated in a specific direction, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used merely to distinguish between descriptions and should not be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal," "vertical," "overhang," and the like do not denote a requirement that the component be absolutely horizontal or overhang, but rather may be slightly inclined. As "horizontal" merely means that its direction is more horizontal than "vertical", and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless explicitly specified and limited otherwise, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
Example 1
Referring to fig. 1, 2 and 3, an embodiment of the present invention provides a sintering flue gas temperature rising denitration device 001, which includes a denitration tower 100 having three layers of denitration catalysts 101 therein, an air inlet flue 110 and an air outlet flue 120 connected with the denitration tower 100, wherein the air inlet flue 110 is connected with an ammonia gas delivery pipe 130 and a flue burner 140 for heating flue gas flowing through the air inlet flue 110, a flue gas-flue gas reheater 150 for heat exchange is connected between the air inlet flue 110 and the air outlet flue 120, the air outlet flue 120 is connected with a desulfurizing tower 160, and a wet electric dust collector 170 is arranged at the top of the desulfurizing tower 160.
The sintering flue gas temperature rising denitration device 001 provided by the embodiment of the invention can effectively utilize the waste heat of the discharged flue gas after denitration treatment, thereby effectively saving energy and playing a role in energy conservation and emission reduction. After the sintering flue gas discharged from the sintering plant enters the denitration tower 100 through the air inlet flue 110, the sintering flue gas is firstly heated to a proper temperature by the flue burner 140, then is mixed with ammonia conveyed by the ammonia conveying pipe 130 and is then introduced to the surface of the denitration catalyst 101 for catalytic reaction to remove nitrogen oxides, then when the high-temperature denitration flue gas is discharged through the air outlet flue 120, the high-temperature denitration flue gas discharged through the air inlet flue 110 and the air outlet flue 120 and the sintering flue gas introduced through the air inlet flue 110 are subjected to first-stage heat exchange treatment through the flue gas-flue gas reheater 150 (namely, a GGH heat exchanger) connected with the air inlet flue 110 and the air outlet flue 120, and the heat of the denitration flue gas is primarily recovered to heat the low-temperature sintering flue gas entering the denitration tower 100, so that the energy consumption of the flue burner 140 is reduced, the heat contained in the denitration flue gas is effectively recovered to save the energy consumed by the flue burner 140, the effect of saving energy is achieved, and then the flue gas cooled by heat exchange is introduced into the desulfurization tower 160, and the wet electric dust collector 170 arranged at the top of the desulfurization tower 160 for dust removal treatment, and the flue gas is subjected to the first-stage heat exchange treatment, and the flue gas pollution emission standard is reduced, and the environmental pollution emission standard is obtained.
The exhaust stack 120 is provided with a primary air preheater 180, and a combustion fan 190 and a stack burner 140 are connected to a first air inlet and a first air outlet of the primary air preheater 180, respectively. The primary air preheater 180 arranged on the exhaust flue 120 can perform heat exchange treatment by using the discharged high-temperature denitration clean flue gas and the combustion air introduced by the combustion fan 190, so that the heated combustion air is introduced into the flue burner 140 for heating, thereby reducing the heating energy consumption of the flue burner 140.
The exhaust flue 120 is further provided with a secondary air preheater 200, and a second air inlet and a second air outlet of the primary air preheater 180 are respectively connected with a desulfurization chimney white air removal fan 210 and an air inlet of the secondary air preheater 200, and an air outlet of the secondary air preheater 200 is communicated with the top of the desulfurizing tower 160. The primary air preheater 180 and the secondary air preheater 200 arranged on the exhaust flue 120 can sequentially use the discharged high-temperature denitration clean flue gas and cold air introduced by the desulfurization chimney white-gas removal fan 210 to perform heat exchange treatment, and the discharged two sections of denitration clean flue gas with different temperatures are used for heating the desulfurization wet chimney white-gas with low temperature to obtain the desulfurization wet chimney white-gas with high temperature, and the heated desulfurization wet chimney white-gas is introduced into the top chimney of the desulfurization tower 160, so that the temperature of the discharged flue gas is increased to perform white removal, and meanwhile, the temperature of the denitration clean flue gas entering the desulfurization tower 160 is reduced to facilitate desulfurization treatment and waste heat recovery, and the effects of energy conservation and emission reduction are realized.
The ammonia gas delivery pipe 130 is connected with a mixer 220, the mixer 220 is connected with a high-temperature dilution fan 230 and an ammonia gas evaporator 240, an inlet of the ammonia gas evaporator 240 is connected with an ammonia water tank 250, an outlet of the ammonia gas evaporator 240 is connected with a wastewater tank 270, and the wastewater tank 270 is connected with a desulfurizing tower 160 through a pipeline. The sintering flue gas introduced by the high-temperature dilution fan 230 is mixed with the ammonia gas prepared by the ammonia evaporator 240 by using the mixer 220, and then the mixture is introduced into the air inlet flue 110 to be mixed with the heated sintering flue gas for further catalytic denitration treatment, so that the mixing uniformity of the ammonia gas and the sintering flue gas can be effectively improved, the denitration effect is improved, the waste water after the ammonia gas is prepared by evaporation of the ammonia evaporator 240 is introduced into the waste water tank 270 for storage, and the waste water is introduced into the desulfurizing tower 160 through a pipeline for ammonia desulfurization, so that the ammonia water waste liquid is fully utilized, the zero emission of the waste water is realized, and the energy conservation and the emission reduction are realized.
The ammonia gas delivery pipe 130 extends into the air inlet flue 110 and is connected with an ammonia spraying grid 260, the ammonia spraying grid 260 is formed by communicating a plurality of hollow ammonia spraying pipes 261, and each ammonia spraying pipe 261 is provided with a plurality of ammonia spraying holes 262. Ammonia gas can be uniformly sprayed into the air inlet flue 110 through the ammonia spraying grille 260 arranged in the air inlet flue 110, and the ammonia gas is uniformly mixed with sintering flue gas and then introduced into the surface catalytic reaction of the denitration catalyst 101 for denitration treatment, so that nitrogen oxides in the sintering flue gas are removed to the greatest extent.
Also installed in the denitration tower 100 is a first pressure reducing plate 280 provided with eight pressure reducing holes, and the first pressure reducing plate 280 is located between the denitration catalyst 101 and the air inlet flue 110. The denitration tower 100 is provided with a first pressure reducing plate 280 located between the denitration catalyst 101 and the air inlet flue 110, which can reduce the flow rate of the sintering flue gas passing through the air inlet flue 110 and passing through the denitration catalyst 101, so that the sintering flue gas mixed with ammonia fully contacts the denitration catalyst 101 to react to remove nitrogen oxides.
A second pressure reducing plate 290 with eight pressure reducing holes is also installed in the air inlet flue 110, and the second pressure reducing plate 290 is located between the flue burner 140 and the ammonia gas conveying pipe 130. The second pressure reducing plate 290 provided between the stack burner 140 and the ammonia gas delivery pipe 130 can reduce the flow rate of the sintering flue gas passing through the gas inlet stack 110 so that the sintering flue gas is sufficiently heated.
The air inlet flue 110, the denitration tower 100 and the air outlet flue 120 are connected to form a figure. The air inlet flue 110, the denitration tower 100 and the exhaust flue 120 are arranged in a shape like a Chinese character 'ji', so that the flue gas-flue gas reheater 150 for heat exchange is connected between the air inlet flue 110 and the exhaust flue 120 for heat exchange, the waste heat loss in the two-stage energy heat exchange recycling process is reduced, and the utilization rate of the waste heat is improved to save energy.
Example 2
Referring to fig. 2, 3 and 4, the embodiment of the invention further provides a sintering flue gas temperature rising denitration system, which includes the sintering flue gas temperature rising denitration device 001, and a third pressure reducing plate 300 provided with eight pressure reducing holes is installed between adjacent denitration catalysts 101, wherein the third pressure reducing plate 300 can reduce the flow rate of the sintering flue gas passing through the denitration catalysts 101, so that the sintering flue gas mixed with ammonia fully contacts the denitration catalysts 101 to react to remove nitrogen oxides.
The first pressure reducing plate 280, the second pressure reducing plate 290 and the third pressure reducing plate 300 are similar in structure and differ only in size ratio.
Example 3
Referring to fig. 1, 2 and 3, an embodiment of the present invention provides a sintering flue gas temperature-rising denitration method, which is implemented by using the sintering flue gas temperature-rising denitration apparatus 001 provided in the above embodiment 1, and mainly includes the following steps:
the sintering flue gas is heated to 250-260 ℃ through heat exchange of a flue gas-flue gas reheater 150 in the air inlet flue 110 and is heated to 300-320 ℃ by a flue burner 140, and then is mixed with the mixed gas of the sintering flue gas and ammonia gas which is introduced by a mixer 220 and is introduced to the surface of a denitration catalyst 101, and the denitration clean flue gas is obtained through catalytic reaction;
the denitration clean flue gas is cooled to 290-300 ℃ through heat exchange of a secondary air preheater 200 arranged on an exhaust flue 120, is cooled to 160-170 ℃ through heat exchange of a flue gas-flue gas reheater 150, is cooled to 150-160 ℃ through heat exchange of a primary air preheater 180, and is subjected to desulfurization and dust removal treatment through a desulfurizing tower 160 to obtain discharged flue gas.
The combustion air is introduced into the primary air preheater 180 to exchange heat with the denitration clean flue gas at 160-170 ℃ so that the combustion air is heated to 130-140 ℃ and then introduced into the flue burner 140 for heating the sintering flue gas.
The white gas of the wet desulfurization chimney is sequentially introduced into the primary air preheater 180 and the secondary air preheater 200 to exchange heat with the denitration flue gas of different temperature sections and the denitration flue gas obtained by catalytic reaction, so that the white gas of the wet desulfurization chimney is sequentially heated to 120-130 ℃ and 200-210 ℃ and then introduced into the chimney at the top of the desulfurizing tower 160 to be mixed with the denitration flue gas of the wet electric dust removal treatment. The white gas of the desulfurization wet chimney is air.
The ammonia gas and the sintering flue gas with the higher temperature are mixed by using the mixer 220, then are mixed with the sintering flue gas heated to 300-320 ℃ by being arranged in the ammonia spraying grid 260 of the air inlet flue 110, and are introduced to the surface of the denitration catalyst 101 for catalytic denitration treatment.
The sintering flue gas temperature rising denitration method provided by the embodiment of the invention can effectively improve the utilization of the tail gas waste heat in the process and remove the nitrogen oxide content in the tail gas to the maximum extent, thereby realizing the effects of energy conservation and emission reduction. The invention selects the medium-temperature SCR denitration process, firstly, the GGH heat exchanger is utilized to recycle the waste heat of the denitration purified flue gas after the denitration treatment, namely, the heat exchange is carried out on the original sintering flue gas, so that the original sintering flue gas is heated to about 260 ℃, and then the denitration treatment is carried out by burning and heating to about 310 ℃, and the heat consumed by burning and heating accounts for 28 percent of the total heat consumption of a direct burning and heating method, thus saving a large amount of energy consumption and reducing the running cost; meanwhile, the GGH heat exchanger and the two-stage air preheater are adopted to recycle the waste heat of the purified flue gas after denitration to carry out the second-stage waste heat recycling, the denitration purified flue gas is used to exchange heat with combustion air and the wet flue gas for desulfurization, so that the waste heat recycling is carried out, the temperature of the denitration purified flue gas can be reduced from 310 ℃ to 160 ℃, the waste heat utilization rate is 83%, the heating SCR denitration technology is combined with the wet flue gas desulfurization and wet flue gas desulfurization technology, the problems of the existing sintering flue gas denitration transformation and wet flue gas desulfurization by wet desulfurization are effectively solved, the energy utilization is optimized through a reasonable design system, and the energy consumption and the cost are greatly reduced.
The detection is carried out after the sintering flue gas temperature rise denitration method and the sintering flue gas temperature rise denitration equipment are actually adopted in the site of the sintering plant, so that NO in the flue gas discharged by the sintering plant can be known X The content of (C) is 100mg/Nm 3 The denitration efficiency is more than 90%, SO 2 The content is 30mg/Nm 3 The dust concentration was below 10mg/Nm 3 The method is characterized by completely meeting and being greatly lower than the national sintering tail gas emission standard.
The sintering flue gas temperature-rising denitration device and the sintering flue gas temperature-rising denitration method provided by the embodiment of the invention can recycle the waste heat contained in the discharged high-temperature denitration flue gas in two stages of energy sources, so that the energy contained in the denitration flue gas is effectively utilized, the energy is recycled to improve the energy utilization rate, and the effects of energy conservation and emission reduction are achieved.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. The sintering flue gas temperature rising denitration method is characterized by comprising the following steps of:
heating sintering flue gas to 300-320 ℃, mixing the sintering flue gas with ammonia gas, introducing the mixture to the surface of a denitration catalyst, and carrying out catalytic reaction to obtain denitration clean flue gas;
the denitration clean flue gas and the sintering flue gas before heating are subjected to heat exchange and cooling to 150-160 ℃, and then are subjected to desulfurization and dust removal treatment to obtain discharged flue gas;
exchanging heat between the denitration flue gas and sintering flue gas before heating, heating the sintering flue gas to 250-260 ℃ and cooling the denitration flue gas to 160-170 ℃; heat exchanging combustion air with denitration clean flue gas cooled to 160-170 ℃ to heat the combustion air to 130-140 ℃ and then heat sintering flue gas, and cooling the denitration clean flue gas to 150-160 ℃; sequentially exchanging heat between the desulfurization wet chimney white-eliminating gas and denitration clean flue gas cooled to 160-170 ℃ and denitration clean flue gas obtained by catalytic reaction, heating the desulfurization wet chimney white-eliminating gas to 200-210 ℃ and then mixing the desulfurization wet chimney white-eliminating gas with wet electric dust removal denitration clean flue gas, cooling the denitration clean flue gas obtained by catalytic reaction to 290-300 ℃ and exchanging heat with sintering flue gas before heating;
mixing ammonia gas with other sintering flue gas, mixing with the sintering flue gas heated to 300-320 ℃ and introducing the mixture to the surface of the catalyst.
2. The sintering flue gas temperature-rising denitration method according to claim 1, wherein NO in the exhaust flue gas X The content is 100mg/Nm 3 The denitration efficiency is more than 90%, SO 2 The content is 30mg/Nm 3 The dust concentration was below 10mg/Nm 3 The following is given.
3. A sintering flue gas temperature-rising denitration device for realizing the sintering flue gas temperature-rising denitration method according to claim 1 or 2, which is characterized by comprising a denitration tower, an air inlet flue and an air outlet flue, wherein the air inlet flue and the air outlet flue are connected with an ammonia conveying pipe and a flue burner for heating flue gas flowing through the air inlet flue, a flue gas-flue gas reheater for heat exchange is connected between the air inlet flue and the air outlet flue, the air outlet flue is connected with a desulfurization tower, and a wet electric dust collector is arranged at the top of the desulfurization tower;
the exhaust flue is provided with a primary air preheater, and a first air inlet and a first air outlet of the primary air preheater are respectively connected with a combustion-supporting fan and the flue burner;
the exhaust flue is also provided with a secondary air preheater, a second air inlet and a second air outlet of the primary air preheater are respectively connected with a desulfurization chimney white air eliminating fan and an air inlet of the secondary air preheater, and the air outlet of the secondary air preheater is communicated with the top of the desulfurization tower.
4. The sintering flue gas temperature-rising denitration device according to claim 3, wherein the ammonia gas conveying pipe is connected with a mixer, the mixer is connected with a high-temperature dilution fan and an ammonia gas evaporator, and an inlet and an outlet of the ammonia gas evaporator are respectively connected with an ammonia water tank and the desulfurizing tower.
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| CN108796215B (en) * | 2018-06-25 | 2019-12-06 | 中南大学 | treatment method of waste desulfurizer |
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| CN109432936A (en) * | 2018-12-04 | 2019-03-08 | 中冶南方都市环保工程技术股份有限公司 | Sintering flue gas processing method and processing system |
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