CN111249873A - Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS - Google Patents
Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS Download PDFInfo
- Publication number
- CN111249873A CN111249873A CN202010118573.XA CN202010118573A CN111249873A CN 111249873 A CN111249873 A CN 111249873A CN 202010118573 A CN202010118573 A CN 202010118573A CN 111249873 A CN111249873 A CN 111249873A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- low
- lime kiln
- scr
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D53/75—Multi-step processes
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- 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
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- 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
Abstract
The invention provides a device and a method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas, wherein the whole system of the SDS dry desulfurization has no industrial water consumption and no waste water, and the moisture content of the kiln flue gas cannot be increased; the desulfurizer is directly sprayed into the flue, a desulfurization tower is not arranged, the resistance of a desulfurization system is not increased, and the energy consumption is low; the SDS desulfurization efficiency reaches more than 95 percent; and has the advantages of low power consumption, low operating cost, small occupied area and the like. The SCR low-temperature denitration process is combined, the low-temperature catalyst is adopted, the front end of a reactor of the low-temperature catalyst does not need a heating device, the rear end of the reactor does not need a waste heat utilization device, the system resistance is only increased by 500-600Pa, the system resistance of the high-temperature catalyst is increased by over 1200Pa, and the equipment cost and the floor area are saved.
Description
Technical Field
The invention relates to the technical field of lime kiln flue gas and waste gas treatment, in particular to a device and a method for SDS (sodium dodecyl sulfate) dry desulfurization and SCR (selective catalytic reduction) low-temperature denitration of lime kiln flue gas.
Background
The lime kiln flue gas waste gas is high-temperature flue gas generated in the production process of the lime kiln, can not be directly discharged according to the environmental protection requirement, and needs to be purified. The lime kiln tail gas has complex components and CO2The content is about 20 percent, N2About 79%, and SO2Harmful gas components such as nitrogen oxides and the like, and a certain amount of dust (about 1-10 g/Nm)3) The main components of the dust are CaO, MgO, C, etc. In addition, the flue gas of the lime kiln tail gas also contains a certain amount of tar.
In the tail gas component of lime kiln, CO2Is a usable component, and SO2Nitrogen oxides, dust and tar belong to pollutants with great harm, and the national emission standards are increasingly strict, which are the key points for treating the tail gas of the lime kiln. The common conventional purification design is wet desulfurization and medium-temperature 320 ℃ SCR denitration process, and under the same yield, the total investment cost of the medium-temperature denitration process is high, and the occupied area and the operation cost are high.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a device and a method for SDS (sodium dodecyl sulfate) dry desulfurization and SCR (selective catalytic reduction) low-temperature denitration of lime kiln flue gas, wherein the whole system of the SDS dry desulfurization has no industrial water consumption and no wastewater, and the moisture content of the kiln flue gas cannot be increased; the desulfurizer is directly sprayed into the flue, a desulfurization tower is not arranged, the resistance of a desulfurization system is not increased, and the energy consumption is low; the SDS desulfurization efficiency reaches more than 95 percent; and has the advantages of low power consumption, low operating cost, small occupied area and the like. The SCR low-temperature denitration process is combined, the low-temperature catalyst is adopted, the front end of a reactor of the low-temperature catalyst does not need a heating device, the rear end of the reactor does not need a waste heat utilization device, the system resistance is only increased by 500-600Pa, the system resistance of the high-temperature catalyst is increased by over 1200Pa, and the equipment cost and the floor area are saved.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
a device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas comprises a desulfurizer raw material bin, a grader, a grinding machine, a finished product desulfurizer storage device and a feeder which are sequentially connected, wherein the feeder is connected with a pipeline of a lime kiln flue gas waste heat boiler, and a flue gas outlet of the lime kiln flue gas waste heat boiler is connected with a dust collector;
the feeding machine is also connected with a fan;
the dust collector is connected with the SCR denitration reactor, and the SCR denitration reactor is connected with the ammonia water storage device.
Preferably, the feeding machine is provided with a nozzle, and the nozzle is connected with the waste heat boiler.
Preferably, the number of the feeding machines is at least 3.
Preferably, the number of the fans is at least 3.
Preferably, a spray gun is arranged at the joint of the dust collector and the SCR denitration reactor.
Preferably, a conveying pump is arranged between the dust collector and the SCR denitration reactor;
preferably, the number of the delivery pumps is at least 3.
A method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas comprises the following steps:
(a) spraying a desulfurizing agent into the flue gas to enable the desulfurizing agent to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
(b) spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the low temperature catalyst is suitably at a reaction temperature of 180-220 ℃.
Preferably, in step (a), the desulfurizing agent is selected from sodium bicarbonate and/or calcium hydroxide;
preferably, the particle size of the desulfurizing agent is 380-400 meshes.
Preferably, in the step (a), in the step of injecting the desulfurizing agent into the flue gas, the temperature of the flue gas is 200-280 ℃.
Preferably, in step (b), the active component of the low-temperature catalyst is vanadium pentoxide.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the device provided by the application, the whole SDS dry desulphurization system has no industrial water consumption and no wastewater, and the moisture content of the kiln flue gas cannot be increased; the desulfurizer is directly sprayed into the flue, a desulfurization tower is not arranged, the resistance of a desulfurization system is not increased, and the energy consumption is low; the SDS desulfurization efficiency reaches more than 95 percent; and has the advantages of low power consumption, low operating cost, small occupied area and the like.
(2) According to the device provided by the application, the SCR low-temperature denitration process adopts the low-temperature catalyst, the front end of a reactor of the low-temperature catalyst does not need a heating device, the rear end of the reactor of the low-temperature catalyst does not need a waste heat utilization device, the system resistance is only increased by 500-600Pa, the system resistance of the high-temperature catalyst is increased by over 1200Pa, and the equipment cost and the floor area are saved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic flow diagram of SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas provided by an embodiment of the present invention.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
A device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas comprises a desulfurizer raw material bin, a grader, a grinding machine, a finished product desulfurizer storage device and a feeder which are sequentially connected, wherein the feeder is connected with a pipeline of a lime kiln flue gas waste heat boiler, and a flue gas outlet of the lime kiln flue gas waste heat boiler is connected with a dust collector;
the feeding machine is also connected with a fan;
the dust collector is connected with the SCR denitration reactor, and the SCR denitration reactor is connected with the ammonia water storage device.
The device that this application provided adopts SDS dry desulfurization technology and SCR low temperature denitration technology to combine together. The whole system of the SDS dry desulphurization does not consume industrial water and generate waste water, and the moisture content of the kiln smoke is not increased; the desulfurizer is directly sprayed into the flue, a desulfurization tower is not arranged, the resistance of a desulfurization system is not increased, and the energy consumption is low; the SDS desulfurization efficiency reaches more than 95 percent; and has the advantages of low power consumption, low operating cost, small occupied area and the like. The SCR low-temperature denitration process adopts the low-temperature catalyst, the front end of a reactor of the low-temperature catalyst does not need a heating device, the rear end of the reactor of the low-temperature catalyst does not need a waste heat utilization device, the system resistance is only increased by 500-600Pa, and the system resistance is increased by more than 1200Pa by the high-temperature catalyst, so that the equipment cost and the floor area are saved.
Preferably, the feeding machine is provided with a nozzle, and the nozzle is connected with the waste heat boiler.
Preferably, the number of the feeding machines is at least 3.
Preferably, the number of the fans is at least 3.
Preferably, a spray gun is arranged at the joint of the dust collector and the SCR denitration reactor.
Preferably, a conveying pump is arranged between the dust collector and the SCR denitration reactor;
preferably, the number of the delivery pumps is at least 3.
A method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas comprises the following steps, wherein the flow is shown in figure 1:
(a) spraying a desulfurizing agent into the flue gas to enable the desulfurizing agent to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
the reaction formula is as follows: SO (SO)2+2NaHCO3＝Na2SO3+H2O+2CO2
Or SO3+2NaHCO3＝Na2SO4+H2O+2CO2；
(b) Spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the reaction formula is as follows: NO +4NH3＝5N2+6H2O or 6NO2+8NH3＝7N2+12H2O；
The low temperature catalyst is suitably at a reaction temperature of 180-220 ℃.
Preferably, in step (a), the desulfurizing agent is selected from sodium bicarbonate and/or calcium hydroxide;
preferably, the particle size of the desulfurizing agent is 380-400 meshes.
Preferably, in the step (a), in the step of injecting the desulfurizing agent into the flue gas, the temperature of the flue gas is 200-280 ℃.
Preferably, in step (b), the active component of the low-temperature catalyst is vanadium pentoxide.
Embodiments of the present invention will be described in detail below with reference to examples, but it will be understood by those skilled in the art that the following examples are only illustrative of the present invention and should not be construed as limiting the scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products commercially available.
Example 1
The method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas provided by the embodiment specifically comprises the following steps:
(a) spraying 380-mesh sodium bicarbonate into the flue gas at 200 ℃ to enable the desulfurizer to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
(b) spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the low-temperature catalyst is suitable for reaction at 180 ℃, and the active component of the low-temperature catalyst is vanadium pentoxide.
Example 2
The method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas provided by the embodiment specifically comprises the following steps:
(a) spraying calcium hydroxide with 400 meshes into the flue gas at 280 ℃ to enable the desulfurizer to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
(b) spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the low-temperature catalyst is suitable for reaction at the temperature of 220 ℃, and the active component of the low-temperature catalyst is vanadium pentoxide.
Example 3
The method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas provided by the embodiment specifically comprises the following steps:
(a) spraying 390-mesh calcium hydroxide into the flue gas at 250 ℃ to enable the desulfurizer to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
(b) spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the low-temperature catalyst is suitable for reaction at the temperature of 200 ℃, and the active component of the low-temperature catalyst is vanadium pentoxide.
Examples of the experiments
In examples 1 to 3, the temperature of flue gas before desulfurization and denitrification: 200 to 280 ℃ SO2≤200mg/m3，NOx≤400mg/m3(ii) a SO can be achieved after desulfurization and denitrification2≤35mg/m3，NOx≤50mg/m3。
While particular embodiments of the present invention have been illustrated and described, it will be appreciated that the above embodiments are merely illustrative of the technical solution of the present invention and are not restrictive; those of ordinary skill in the art will understand that: modifications may be made to the above-described embodiments, or equivalents may be substituted for some or all of the features thereof without departing from the spirit and scope of the present invention; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; it is therefore intended to cover in the appended claims all such alternatives and modifications that are within the scope of the invention.
Claims (10)
1. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas is characterized by comprising a desulfurizer raw material bin, a classifier, a grinding machine, a finished product desulfurizer storage device and a feeder which are sequentially connected, wherein the feeder is connected with a pipeline of a lime kiln flue gas waste heat boiler, and a flue gas outlet of the lime kiln flue gas waste heat boiler is connected with a dust collector;
the feeding machine is also connected with a fan;
the dust collector is connected with the SCR denitration reactor, and the SCR denitration reactor is connected with the ammonia water storage device.
2. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 1, wherein a nozzle is arranged on the feeder and connected with the exhaust-heat boiler.
3. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 1, wherein the number of the feeders is at least 3.
4. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 1, wherein the number of the fans is at least 3.
5. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 1, wherein a spray gun is arranged at the joint of the dust collector and the SCR denitration reactor.
6. The device for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 1, wherein a delivery pump is arranged between the dust collector and the SCR denitration reactor;
preferably, the number of the delivery pumps is at least 3.
7. A method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas is suitable for the device for SDS dry desulfurization and SCR low-temperature denitration of the lime kiln flue gas according to any one of claims 1 to 6, and is characterized by comprising the following steps of:
(a) spraying a desulfurizing agent into the flue gas to enable the desulfurizing agent to react with sulfur dioxide in the flue gas to generate sodium sulfate solid, water and carbon dioxide, thereby completing flue gas desulfurization;
(b) spraying urea into the flue gas treated in the step (a), generating ammonia gas under the action of the waste heat of the flue gas, and carrying out chemical reaction on the ammonia gas and nitric oxide in the flue gas under the action of a low-temperature catalyst to generate nitrogen gas and water so as to complete flue gas denitration;
the low temperature catalyst is suitably at a reaction temperature of 180-220 ℃.
8. The method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas according to claim 7, wherein in step (a), the desulfurizing agent is selected from sodium bicarbonate and/or calcium hydroxide;
preferably, the particle size of the desulfurizing agent is 380-400 meshes.
9. The method for SDS dry desulfurization and SCR low-temperature denitration of lime kiln flue gas as recited in claim 7, wherein in the step (a), the temperature of the flue gas in the step of injecting the desulfurizing agent into the flue gas is 200-280 ℃.
10. The method for desulfurizing and denitrating the flue gas of the lime kiln according to claim 7, wherein in the step (b), the active component of the low-temperature catalyst is vanadium pentoxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010118573.XA CN111249873A (en) | 2020-02-26 | 2020-02-26 | Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010118573.XA CN111249873A (en) | 2020-02-26 | 2020-02-26 | Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111249873A true CN111249873A (en) | 2020-06-09 |
Family
ID=70945774
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010118573.XA Pending CN111249873A (en) | 2020-02-26 | 2020-02-26 | Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111249873A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113371735A (en) * | 2021-07-05 | 2021-09-10 | 浙江致远环境科技有限公司 | Process and device for producing anhydrous sodium sulphate by using sulfur dioxide in waste gas |
| CN114345120A (en) * | 2021-12-16 | 2022-04-15 | 中煤科工集团西安研究院有限公司 | Novel ultralow emission device and process for flue gas pollutants in dry cement process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108201781A (en) * | 2017-12-27 | 2018-06-26 | 武汉都市环保工程技术股份有限公司 | Coke oven flue gas comprehensive treatment system based on sodium backbone method and low temperature SCR denitration |
| CN110614028A (en) * | 2019-08-28 | 2019-12-27 | 江苏新中金环保科技股份有限公司 | Low-temperature flue gas SO in cement kiln2、NOxAnd Hg0Cooperative control system and method |
-
2020
- 2020-02-26 CN CN202010118573.XA patent/CN111249873A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108201781A (en) * | 2017-12-27 | 2018-06-26 | 武汉都市环保工程技术股份有限公司 | Coke oven flue gas comprehensive treatment system based on sodium backbone method and low temperature SCR denitration |
| CN110614028A (en) * | 2019-08-28 | 2019-12-27 | 江苏新中金环保科技股份有限公司 | Low-temperature flue gas SO in cement kiln2、NOxAnd Hg0Cooperative control system and method |
Non-Patent Citations (2)
| Title |
|---|
| 上海市环境保护工业行业协会: "《工业大气污染防治技术及应用》", 30 November 2016, 上海科学技术出版社 * |
| 贾华平: "《水泥生产技术与实践》", 31 January 2018, 中国建材工业出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113371735A (en) * | 2021-07-05 | 2021-09-10 | 浙江致远环境科技有限公司 | Process and device for producing anhydrous sodium sulphate by using sulfur dioxide in waste gas |
| CN114345120A (en) * | 2021-12-16 | 2022-04-15 | 中煤科工集团西安研究院有限公司 | Novel ultralow emission device and process for flue gas pollutants in dry cement process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107983119A (en) | The dry desulfurization method of denitration of oxidation is forced based on ozone | |
| CN110756033A (en) | Deep purification treatment system and process for waste incineration power station flue gas | |
| CN102008893A (en) | Low temperature SCR moving bed flue gas denitration method for coal-fired boiler | |
| CN110860196A (en) | Desulfurization and denitrification system for cement flue gas | |
| CN211886232U (en) | Sodium-based dry desulfurization system applied to low-sulfur flue gas working condition | |
| CN105056758A (en) | Method for fluidized catalytic removal of nitrogen oxide, and apparatus thereof | |
| WO2021088526A1 (en) | Flue gas multi-pollutant synergistic purification process and apparatus | |
| CN111249873A (en) | Device and method for dry desulfurization and SCR low-temperature denitration of lime kiln flue gas SDS | |
| CN210631915U (en) | Cement kiln desulfurization system | |
| CN104998539A (en) | Dry flue gas desulfurization, denitrification and dedusting integrated purification process | |
| CN205308112U (en) | Ozone and device of air in coordination with nitrogen oxide in oxidation flue gas | |
| CN202387362U (en) | Semi-dry low temperature flue gas denitrification system | |
| CN109260919A (en) | The integration desulfurization denitration device and its desulfurization denitration method of ozone combination urea | |
| CN210464078U (en) | Smelting flue gas treatment system | |
| CN108339385A (en) | The double tower ammonia process of desulfurization organically combines the method for sintering flue gas desulfurization denitration with oxidation catalysis denitration | |
| CN113117478A (en) | Flue gas desulfurization and denitrification method based on fly ash | |
| CN217220890U (en) | Domestic waste burns flue gas denitration deacidification dust removal integration system of optimization | |
| CN203281209U (en) | Flue gas denitration system by adopting SNCR and SCR combination method for coal-fired boiler | |
| CN104941417A (en) | Flue gas treatment device and method | |
| CN213668653U (en) | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower | |
| WO2021134927A1 (en) | Dry process of integrated flue gas desulfurization and denitration | |
| CN102698600A (en) | System for intelligently controlling flue gas denitrification of cement plant based on selective catalytic reduction (SCR) method | |
| CN102350189B (en) | Half-dry low-temperature smoke denitrification system | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN106853320A (en) | A kind of coal-burning boiler for flue gas desulfurization, denitration mechanism and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200609 |
|
| RJ01 | Rejection of invention patent application after publication |