CN1712115A - High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof - Google Patents
High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof Download PDFInfo
- Publication number
- CN1712115A CN1712115A CN 200510034441 CN200510034441A CN1712115A CN 1712115 A CN1712115 A CN 1712115A CN 200510034441 CN200510034441 CN 200510034441 CN 200510034441 A CN200510034441 A CN 200510034441A CN 1712115 A CN1712115 A CN 1712115A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- flue gas
- desulfurizer
- reaction tower
- desulfurization
- 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.)
- Granted
Links
Images
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
An efficient catalytic process for desulfurizing and denitrifying fume includes such steps as spraying Fe-base catalyst, desulfurizing agent Ca(OH)2 and denitrifying agent NH3 into flue, mixing in fume reaction tower, spraying the solution of Fe-base catalyst, and reacting for desulfurizing and denitrifying the the fume. Its system is also disclosed.
Description
Technical Field
The invention relates to a method and a device for desulfurizing and denitrifying in flue gas, in particular to a method and a device for removing sulfur dioxide and nitrogen oxide in flue gas discharged from coal-fired, oil-fired and gas-fired boilers.
Background
As harmful gases such as sulfur dioxide, nitrogen oxide and the like in flue gas generated during coal burning, fuel oil and fuel gas are discharged into the atmosphere to cause acid rain, destroy the ecological environment and influence the body health of people, relevant environmental protection regulations in China put forward strict control standard requirements on the allowable emission concentration of the sulfur dioxide and the nitrogen oxide in the flue gas, various methods and devices for desulfurization and denitrification are produced in response.
In the prior control method of the atmospheric pollutants in China, particularly in the technical field of flue gas desulfurization and denitrification, the problems that ① has more independent desulfurization technologies and less desulfurization and denitrification technologies, ② has large investment, high energy consumption and high operating cost, most of ③ desulfurization residues are abandoned and cannot be directly utilized or recycled, so that solid waste is increased, and even a large amount of industrial wastewater is generated exist.
In the wet desulfurization technique, taking limestone-gypsum method as an example: the desulfurization efficiency can reach 95 percent, but the denitrification can not be simultaneously carried out, the desulfurization system is easy to corrode, the investment is high, the operating cost is high, the energy consumption is high, the desulfurization slag is dihydrate gypsum and can not be directly utilized, and simultaneously, the generated industrial wastewater needs to be treated.
Chinese patent with application number 200310103954.7, publication number CNl539546A and invention name 'a flue gas desulfurization and denitrification purification method and device' discloses a flue gas desulfurization and denitrification purification method and device. The purification method of the invention is to spray a high-activity absorbent into the circulating fluidized bed reactor to absorb the sulfur dioxide SO in the flue gas2With nitrogen oxides NOx(ii) a The high-activity absorbent which is not completely reacted is sent back to the feeding pipe for recycling by utilizing a material return leg on the dust removal device. The device comprises a circulating fluidized bed reactor, a dust removal device, a water spraying humidifying device and a feeding device. The invention can remove sulfur and nitrogen simultaneously, and sulfur dioxide SO can be removed under the condition that the calcium-sulfur-nitrogen ratio Ca/(S + N) is 1.12The removal efficiency of the catalyst is more than 90 percent, and the nitrogen oxide NO isxThe removal efficiency is more than 60%. This patent has the following problems: (1) the high-activity absorbent is uniformly mixed by adding water, stirred, centrifugally dewatered and dried, hardened and difficult to spray into a reactor, and if the high-activity absorbent is ground again, the cost is inevitably increased, and the high-activity absorbent is difficult to popularize and use. (2) The additives are expensive chemical raw materials, and can generate new pollutants after reaction, thereby being environment-friendlyIs not very friendly. (3) The desulfurization and denitrification efficiency respectively reaches more than 90 percent and more than 60 percent, the relative efficiency is low, the desulfurization and denitrification efficiency is not suitable for medium and high sulfur coal, and the desulfurization and denitrification efficiency cannot adapt to increasingly strict environmental protection requirements.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide the high-efficiency catalytic flue gas desulfurization and denitrification method which can realize desulfurization and denitrification, has high efficiency, moderate investment, low operating cost and no wastewater discharge and can completely recycle desulfurized slag.
The invention also aims to provide a device for realizing the high-efficiency catalytic flue gas desulfurization and denitrification method.
The technical scheme adopted for solving the technical problems is as follows:
a high-efficiency catalytic desulfurizing and denitrifying method for fume features that the iron-base catalyst and desulfurizing agent Ca (OH) are sprayed in the fume channel2Denitrifier ammonia NH3Mixing, feeding into flue gas reaction tower, spraying iron-base catalyst solution into the reaction tower, and fully reacting at 80-300 deg.C to realize desulfurization and denitrification.
Under the action of catalyst, ammonia NH3With nitrogen oxides NO in the flue gasxReaction to produce nitrogen gas N2The main chemical reaction is:
sulfur dioxide SO in flue gas2Is mostly converted into sulfur trioxide (SO) under the action of a catalyst3And with calcium hydroxide Ca (OH)2React to generate calcium sulfate CaSO4The main chemical reactionformula is as follows:
the following reactions are carried out on harmful gases such as hydrogen chloride HCl, hydrogen fluoride HF and the like in the flue gas:
the iron-based catalyst is ferrous sulfate FeSO4·H2O and potassium permanganate KMnO4The weight percentage content is as follows: ferrous sulfate FeSO4·H2O accounts for 80-95 percent, and potassium permanganate KMnO 45 to 20 percent; the injection amount of the iron-based catalyst is adjusted according to the measurement of 2-10% of the desulfurization agent amount.
The iron-based catalyst solution takes water as a solvent, the iron-based catalyst is a solute, the weight percentage concentration of the iron-based catalyst is 1.2% -5%, and the spraying amount of the iron-based catalyst solution is automatically adjusted according to the water adding amount required by the temperature control of the reactor.
The desulfurizing agent is calcium hydroxide Ca (OH)2The addition amount of the sulfur-containing additive is adjusted according to the content of sulfur in the flue gas, and when the molar ratio of calcium to sulfur is 1.2-1.4, the desulfurization efficiency can reach 96-97%.
The adding amount of the denitrified ammonia gas is adjusted according to the content of the nitrogen oxides in the flue gas, when the molar ratio of ammonia to the nitrogen oxides is 0.75-1.0, the denitrification efficiency can reach 86% -88%, and the escape value of ammonia is less than 5 multiplied by 10-6。
The technical scheme adopted by the invention for solving the other technical problem is as follows:
the device for realizing the high-efficiency catalytic flue gas desulfurization and denitrification method independently or simultaneously comprises the following steps:
a reaction tower, main reaction equipment for desulfurization and denitrification;
a pre-dust collector for removing dust from the flue gas discharged from the boiler;
a desulfurizing agent storage for storing a desulfurizing agent;
the bin top dust remover is positioned at the top of the desulfurizer bin and is used for purifying the escaped gas when the desulfurizer bin is fed;
the desulfurizer pneumatic conveying pump is used for conveying the desulfurizer in the desulfurizer bin to the pre-deduster and the flue of the reaction tower;
an ammonia tank for storing liquid ammonia;
an ammonia evaporator for heating and evaporating liquid ammonia to ammonia gas for introduction into a flue between the pre-dust collector and the reaction tower;
a catalyst storage for storing catalyst;
a catalyst pneumatic conveying pump for conveying the catalyst;
a catalyst silo for temporarily storing the catalyst for metering;
a distribution transmitter for conveying the catalyst in two paths; one path of the catalyst is conveyed to a pre-deduster and a fluebetween reaction towers; the other path conveys the catalyst to the small catalyst bin;
a catalyst metering adjustable screw for metering and adjusting the adding amount of the catalyst;
a catalyst liquid agitation tank to dissolve the homogenized catalyst;
a water feeder, which adds water into the catalytic liquid stirring tank to dissolve the catalyst into catalytic liquid;
a water pump for pumping the catalytic liquid into the reaction tower;
a dust remover for purifying the flue gas discharged from the reaction tower;
the powder concentrator is used for grading the particle size of the powdery material collected by the dust remover;
a chain conveyer for conveying the dust collected by the dust collector to the powder concentrator;
a circulating pneumatic conveying pump for feeding the fine powder desulfurizer separated by the powder concentrator back to the reaction tower;
a desulfurizing slag bin for temporarily storing desulfurizing slag;
a top dust remover positioned at the top of the desulfurization slag bin and used for purifying gas escaping from the desulfurization slag bin during feeding;
the pneumatic desulfurization slag conveying pump is used for conveying the desulfurization slag separated by the powder concentrator to the desulfurization slag bin;
the induced draft fan is used for providing fluid power for the whole flue gas treatment system;
a chimney for discharging the purified flue gas into the atmosphere;
and the DCS control system tracks according to the signal of the gas on-line monitor and adjusts the temperature, pressure, current and various material quantities of the system so as to form closed-loop automatic control.
The reaction tower is internally provided with a load adjusting plug.
An inner separator is arranged in front of an outlet at the upper part in the reaction tower and separates the desulfurizer and the purified gas, so that the reaction tower can keep higher concentration of the desulfurizer.
The working process of the invention is as follows: the flue gas discharged from the boiler passes through a pre-deduster and enters a reaction tower, and the iron-based catalyst sent by a distribution transmitter and the calcium-based desulfurizer sprayed by a desulfurizer pneumatic conveying pump or/and ammonia introduced by an ammonia evaporator are added in the middle. In the reaction tower, under the action of the airflow field, the catalyst, the desulfurizer or/and ammonia, sulfur dioxide and nitrogen oxide are fully mixed to produce physical and chemical reactions, transfer mass and heat, and the reactions of desulfurization and/or denitrification are completed; the airflow enters the dust remover through the inner separator, and the purified gas is discharged into a chimney by a draught fan and returns to the atmospheric environment.
The powdery material collected by the dust remover enters the powder concentrator through the chain conveyor, the separated coarse particles, namely the fluidized slag calcium sulfate, are conveyed to the desulfurization slag bin for sale by the desulfurization slag pneumatic conveying pump, and the redundant gas is purified by the bin top dust remover and then discharged.
The fine particles separated by the powder concentrator, namely the desulfurizer, are sent into the reaction tower through the circulating pneumatic conveying pump to continuously participate in the reaction, thus forming circulation.
The inner separator is an inertia conical separator in front of an outlet at the upper part in the reaction tower, so that higher concentration of the desulfurizer in the reaction tower can be kept.
The load adjusting plug is A, B two working positions in the reaction tower, and is at A position when the reaction tower is fully loaded; when the load is low, the load adjusting plug is positioned at the position B, so that the throat of the reaction tower keeps a certain air flow speed, and the reaction efficiency is ensured. The load adjusting plug is hung in the reaction tower by a stainless steel wire rope and can be adjusted up and down according to the load.
The catalyst bin is characterized in that an iron-based catalyst is conveyed to an outlet flue of a pre-deduster through a catalyst pneumatic conveying pump and a distribution transmitter, one part of the catalyst is conveyed to a small catalyst bin, the other part of the catalyst is conveyed to a catalytic liquid stirring tank through a catalyst metering adjustable screw, water is added into the tank, the catalytic liquid with a certain concentration is formed after stirring and dissolving uniformly, and the catalytic liquid is sprayed into a reaction tower through a water pump, so that catalytic reaction is realized.
The control of the whole device is realized by a 27DCS control system, and the temperature, the pressure, the current and various material quantities of the system are tracked and adjusted according to the signal of the gas on-line monitor in the chimney, so that the closed-loop automatic control is formed, and the stable and efficient operation is realized.
The invention has the beneficial effects that:
1. the device of the invention can simultaneously desulfurize and denitrify and can independently desulfurize or denitrify. When the ammonia tank and the ammonia evaporator are removed or stopped, the desulfurization can be carried out independently; when the desulfurizer pneumatic conveying pump, the desulfurizer bin, the bin top dust remover, the circulating pneumatic conveying pump, the powder concentrator, the desulfurization slag pneumatic conveying pump, the desulfurization slag bin and the bin top dust remover are removed or stopped to be used, the independent denitrification can be realized.
2. The method has high desulfurization and denitrification efficiency, and the desulfurization efficiency can reach 96-97% when the molar ratio of calcium to sulfur is 1.2-1.4; when the molar ratio of ammonia to nitrogen oxide is 0.75-1.0, the denitrification efficiency can reach 86% -88%, and the escape value of ammonia is less than 5 multiplied by 1O-6. The desulfurized slag is calcium sulfate hemihydrate with the content of 97-98 percent and can be directly utilized. No waste water is discharged.
3. The method and the device are suitable for the flue gas desulfurization and denitrification of coal-fired, gas-fired and oil-fired boilers.
Drawings
FIG. 1 is a device for implementing the high-efficiency catalytic flue gas desulfurization and denitrification method of the invention
Detailed description of the preferred embodiment
Example 1
As shown in figure 1, the device for realizing the catalytic flue gas desulfurization and denitrification method comprises the following steps:
a reaction tower 5, main reaction equipment for desulfurization and denitrification;
a load adjusting plug 6, which has A, B two working positions in the reaction tower, and is at A position when the reaction tower is at full load; when the load is low, the load adjusting plug is positioned at the position B, so that the throat of the reaction tower 5 keeps a certain air flow speed, and the reaction efficiency is ensured. The load adjusting plug is hung in the reaction tower by a stainless steel wire rope and can be adjusted up and down according to the load;
an inner separator 7, located in front of the upper outlet of the reaction tower 5, for separating most of the desulfurizer from the purified gas, so as to maintain a higher concentration of desulfurizer in the reaction tower 5;
a pre-dust collector 1 for removing dust from the flue gas discharged from the boiler;
a desulfurizing agent storage 3 for storing a desulfurizing agent;
a top dust collector 4 positioned at the top of the desulfurizer bin 3 and used for purifying the escaping gas when the desulfurizer bin is fed;
a desulfurizer pneumatic conveying pump 2 used for conveying the desulfurizer in the desulfurizer bin 3 to a flue between the pre-deduster 1 and the reaction tower 5;
an ammonia tank 25 for storing liquid ammonia;
an ammonia evaporator 26 for heating and evaporating liquid ammonia into ammonia gas to be introduced into a flue between the pre-dust collector 1 and the reaction tower 5;
a catalyst storage 20 for storing catalyst;
a catalyst pneumatic conveying pump 21 for conveying the catalyst;
a catalyst silo 17 for temporarily storing the catalyst for metering;
a distribution transmitter 22 for conveying the catalyst in two paths; onepath of the catalyst is conveyed to a flue between a pre-deduster 1 and a reaction tower 5; the other path conveys the catalyst to the small catalyst bin 17;
a catalyst metering adjustable screw 18 for metering and adjusting the adding amount of the catalyst;
a catalyst liquid agitation tank 19 for dissolving the homogenized catalyst;
a water feeder 23 for feeding water into the catalyst solution agitation tank 19 to dissolve the catalyst into the catalyst solution;
a water pump 24 for pumping the catalytic liquid into the reaction tower 5;
a dust collector 10 for purifying the flue gas discharged from the reaction tower 5;
a powder selecting machine 9 for grading the particle size of the powdery material collected by the dust remover 10;
a chain conveyor 11 for conveying the dust collected by the dust collector 10 to the powder concentrator 9;
a circulating pneumatic conveying pump 8 for returning the fine powder desulfurizer separated by the powder concentrator 9 to the reaction tower 5;
a desulfurized slag bin 14 for temporarily storing desulfurized slag;
a top dust remover 15 which is arranged at the top of the desulfurized slag bin 14 and is used for purifying gas escaping from the desulfurized slag bin 15 during feeding;
a desulfurized slag pneumatic conveying pump 12 for conveying the desulfurized slag separated by the powder concentrator 9 to the desulfurized slag bin 14;
an induced draft fan 13 for providing fluid power to the whole flue gas treatment system;
a chimney 16 for exhausting the purified flue gas to the atmosphere;
and a DCS control system 27 for tracking according to the signal of the gas on-line monitor and adjusting the temperature, pressure, current and various material quantities of the system so as to form closed-loop automatic control.
Example 2
The device of example 1 is used for treating the flue gas of a pulverized coal fired boiler of a power plant at 410t/h, the original electric precipitator is used as a pre-precipitator, and the desulfurizer is calcium hydroxide Ca (OH)2The denitrifier is ammonia NH3(ii) a The iron-based catalyst is FeSO with the weight percentage of ferrous sulfate being 80 percent4·H2O and 20% potassium permanganate KMnO4The sprayed amount of the mixture is 10 percent of the weight of the desulfurizer, and the iron-based catalyst is aqueous solution with the weight percentage concentration of 3 percent. After the apparatus of example 1 was used, the reaction temperature in the reaction tower was set to 80 ℃ and the desulfurization efficiency reached 96.5% when the calcium/sulfur molar ratio was 1.28; when the molar ratio of ammonia to nitrogen oxide is O.8, the denitrification efficiency reaches 87%; the desulfurized slag contains 97 percent of calcium sulfate hemihydrate; the smoke emission concentration is less than 35 mg/standard meter; no wastewater discharge; the aims of desulfurization and denitrification are achieved simultaneously; the running cost is increased by 1.3 minutes RMB per degree of electricity.
Example 3
The apparatus of example 1 was used for the treatment of flue gas from a gas-fired boiler, the desulfurizing agent being calcium hydroxide Ca (OH)2The denitrifier is ammonia NH3(ii) a The iron-based catalyst is FeSO with the weight percentage of ferrous sulfate of 95 percent4·H2O and 5% potassium permanganate KMnO4The spraying amount of the mixture is 2 percent of the weight of the desulfurizer, and the iron-based catalyst is aqueous solution with the weight percentage concentration of 1.2 percent. After the apparatus of example 1 was used, the reaction temperature in the reaction tower was set to 200 ℃ and the desulfurization efficiency reached 96% when the calcium/sulfur molar ratio was 1.20; when the molar ratio of ammonia to nitrogen oxide is 1.0, the denitrification efficiency reaches 88 percent; the desulfurized slag contains 98 percent of calcium sulfate hemihydrate; the smoke emission concentration is less than 30 mg/standard meter; no wastewater discharge; realizes the aims of desulfurization and denitrification simultaneously.
Example 4
The device of example 1 is used for treating the flue gas of an oil-fired boiler and desulfurizing agentIs calcium hydroxide Ca (OH)2The denitrifier is ammonia NH3(ii) a The iron-based catalyst is FeSO with the weight percentage of ferrous sulfate being 90 percent4·H2O and 10% potassium permanganate KMnO4The spraying amount of the mixture is 5 percent of the weight of the desulfurizer, and the iron-based catalyst is aqueous solution with the weight percentage concentration of 5 percent. After the device of example 1 was used, the reaction temperature in the reaction tower was set to 300 ℃, and when the calcium/sulfur molar ratio was 1.40, the desulfurization efficiency reached 97%; when the molar ratio of ammonia to nitrogen oxide is 0.75, the denitrification efficiency reaches 86 percent; the desulfurized slag contains 97.5 percent of calcium sulfate hemihydrate; the smoke emission concentration is less than 30 mg/standard meter; no wastewater discharge; realizes the aims of desulfurization and denitrification simultaneously.
Claims (8)
1. A high-efficiency catalytic flue gas desulfurization and denitrification method is characterized in that: spraying iron-based catalyst and desulfurizer calcium hydroxide Ca (OH) into the flue2Denitrifier ammonia NH3(ii) a Mixing the mixture and entering a flue gas reaction tower, and spraying an iron-based catalyst solution into the reaction tower; fully reacting under the working condition that the temperature is 80-300 ℃, and realizing simultaneous desulfurization and denitrification;
the iron-based catalyst is ferrous sulfate FeSO4·H2O and potassium permanganate KMnO4The mixture comprises the following components in percentage by weight: ferrous sulfate FeSO4·H2O accounts for 80-95 percent, and potassium permanganate KMnO45 to 20 percent; the injection amount of the iron-based catalyst is adjusted according to the measurement of 2-10 percent of the weight percentage of the desulfurizer.
2. The high-efficiency catalytic flue gas desulfurization and denitrification method according to claim 1, wherein: the iron-based catalyst solution is an aqueous solution, and the weight percentage concentration of the iron-based catalyst solution is 1.2-5%.
3. The high-efficiency catalytic flue gas desulfurization and denitrification method according to claim 1, wherein: spraying iron-based catalyst and desulfurizer calcium hydroxide Ca (OH) into the flue2And denitrificationAgent NH3Before, the flue gas is dedusted by a pre-deduster.
4. The high-efficiency catalytic flue gas desulfurization and denitrification method according to claim 1, wherein: the desulfurizing agent calcium hydroxide Ca (OH)2The addition amount of the calcium carbonate is adjusted according to the content of sulfur in the flue gas, and the molar ratio of calcium to sulfur is 1.2-1.4.
5. The high-efficiency catalytic flue gas desulfurization and denitrification method according to claim 1, wherein: the denitrifier is ammonia NH3The adding amount of the catalyst is adjusted according to the content of nitrogen oxides in the flue gas, and the molar ratio of ammonia to the nitrogen oxides is 0.75-1.0.
6. An apparatus for carrying out the catalytic flue gas desulfurization and denitrification process according to any one of claims 1 to 5, comprising:
a reaction tower (5), main reaction equipment for desulfurization and denitrification;
a pre-dust collector (1) for removing dust from flue gas discharged from a boiler;
a desulfurizer bin (3) for storing desulfurizer;
a top dust remover (4) is positioned at the top of the desulfurizer bin (3) and is used for purifying the escaped gas when the desulfurizer bin is fed;
a desulfurizer pneumatic conveying pump (2) which is used for conveying the desulfurizer in the desulfurizer bin (3) to the flue of the reaction tower (5) from the pre-deduster (1);
an ammonia tank (25) for storing liquid ammonia;
an ammonia evaporator (26) for heating and evaporating liquid ammonia into ammonia gas for introduction into the pre-precipitator (1)
A flue to the reaction tower (5);
a catalyst storage (20) for storing catalyst;
a catalyst pneumatic conveying pump (21) for conveying the catalyst;
a catalyst silo (17) for temporarily storing the catalyst for metering;
a distribution transmitter (22) for conveying the catalyst in two paths; one path of the catalyst is conveyed to a flue between the pre-deduster (1) and the reaction tower (5); the other path conveys the catalyst to the small catalyst bin (17);
a catalyst metering adjustable screw (18) for metering and adjusting the adding amount of the catalyst;
a catalyst liquid agitation tank (19) for dissolving the homogenized catalyst;
a water feeder (23) for feeding water into said catalyst solution agitation tank (19) to dissolve the catalyst into the catalyst solution;
a water pump (24) for pumping the catalytic liquid into the reaction tower (5);
a dust separator (10) for purifying the flue gas discharged from said reaction column (5);
a powder concentrator (9) for classifying the particle size of the powdery material collected by the dust collector (10);
a chain conveyor (11) for conveying the dust collected by the dust collector (10) to the powder concentrator (9);
a circulating pneumatic conveying pump (8) for returning the fine powder desulfurizer separated by the powder concentrator (9) to the reaction tower (5);
a desulfurized slag bin (14) for temporarily storing desulfurized slag;
a top dust remover (15) arranged at the top of the desulfurization slag bin (14) and used for purifying gas escaping from the desulfurization slag bin (15) during feeding;
a desulfurized slag pneumatic conveying pump (12) which is used for conveying the desulfurized slag separated by the powder concentrator (9) to the desulfurized slag bin (14);
an induced draft fan (13) for providing fluid power to the whole flue gas treatment system;
a chimney (16) for exhausting the purified flue gas to the atmosphere;
and a DCS control system (27) for tracking according to the signal of the gas on-line monitor and adjusting the temperature, pressure, current and various material quantities of the system so as to form closed-loop automatic control.
7. The apparatus of claim 6, wherein: a load adjusting plug (6) is arranged in the reaction tower (5).
8. The apparatus of claim 6 or 7, wherein: an inner separator (7) is arranged in front of an outlet at the upper part in the reaction tower (5), and the desulfurizing agent is separated from the purified gas by the inner separator (7), so that the reaction tower (5) is kept at a higher desulfurizing agent concentration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100344414A CN1327939C (en) | 2005-05-09 | 2005-05-09 | High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100344414A CN1327939C (en) | 2005-05-09 | 2005-05-09 | High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1712115A true CN1712115A (en) | 2005-12-28 |
| CN1327939C CN1327939C (en) | 2007-07-25 |
Family
ID=35718017
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100344414A Expired - Fee Related CN1327939C (en) | 2005-05-09 | 2005-05-09 | High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1327939C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101279186B (en) * | 2008-05-23 | 2011-05-11 | 清华大学 | Flue gas dry-type method for simultaneously desulfurizing and denitrating |
| CN102247750A (en) * | 2011-07-11 | 2011-11-23 | 华东理工大学 | Device and method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process |
| CN102824844A (en) * | 2012-09-11 | 2012-12-19 | 北京世能中晶能源科技有限公司 | Desulfurization and denitrification agent, preparation method and application thereof |
| CN101397514B (en) * | 2007-09-30 | 2012-12-19 | 孟小平 | Quick-burning clean coal fines and method for producing the same |
| CN111330439A (en) * | 2020-03-25 | 2020-06-26 | 韩建英 | Catalytic oxidation desulfurization method for ship flue gas |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3701527A1 (en) * | 1987-01-21 | 1988-08-04 | Metallgesellschaft Ag | METHOD FOR SIMULTANEOUS NICKELING AND DESULFURATION OF AN OXYGEN-EXHAUST GAS |
| JPH06210138A (en) * | 1992-11-26 | 1994-08-02 | Nippon Steel Corp | Dry exhaust gas purifying method and operation of blast furnace and sintering machine |
| CN1247294C (en) * | 2003-11-02 | 2006-03-29 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
| CN1234445C (en) * | 2003-11-05 | 2006-01-04 | 余鸿 | Calcium spraying catalytic desulfurization method in pulverized coal fired boiler and device thereof |
| CN1562479A (en) * | 2004-03-16 | 2005-01-12 | 沈阳大学 | Adsorptive catalyst for desulfurization and denitrogenation of coal smoke |
| CN1232620C (en) * | 2004-06-02 | 2005-12-21 | 刘汉东 | Catalytic coal desulfurizer and preparing method thereof |
-
2005
- 2005-05-09 CN CNB2005100344414A patent/CN1327939C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101397514B (en) * | 2007-09-30 | 2012-12-19 | 孟小平 | Quick-burning clean coal fines and method for producing the same |
| CN101279186B (en) * | 2008-05-23 | 2011-05-11 | 清华大学 | Flue gas dry-type method for simultaneously desulfurizing and denitrating |
| CN102247750A (en) * | 2011-07-11 | 2011-11-23 | 华东理工大学 | Device and method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process |
| CN102247750B (en) * | 2011-07-11 | 2014-04-09 | 华东理工大学 | Method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process |
| CN102824844A (en) * | 2012-09-11 | 2012-12-19 | 北京世能中晶能源科技有限公司 | Desulfurization and denitrification agent, preparation method and application thereof |
| CN111330439A (en) * | 2020-03-25 | 2020-06-26 | 韩建英 | Catalytic oxidation desulfurization method for ship flue gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1327939C (en) | 2007-07-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1038312C (en) | Dry processes for treating combustion exhaust gas | |
| CN1962034A (en) | Method and apparatus for removing sulfur, nitrate and mercury simultaneously from boiler flue gas | |
| CN203436995U (en) | Cooperative control device for multi-pollutant in sintering flue gas | |
| CN101073741A (en) | Method and apparatus for combined removing sulfur-dioxide and nitrogenoxide by mixed solution | |
| CN101053738A (en) | Wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction and system thereof | |
| CN1247294C (en) | Method and equipment of desulfurization and denitrogenation for purifying flue gas | |
| US20150265965A1 (en) | Flue gas treatment apparatus and flue gas treatment method | |
| CN101342459A (en) | Exhuast gas desulfurization, recycle and treatment method and apparatus | |
| WO2016011682A1 (en) | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of sintering flue gas | |
| CN1712115A (en) | High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof | |
| CN111359422A (en) | Efficient dry deacidification device and method for waste incineration flue gas | |
| CN111068504A (en) | Method and device for removing heavy metal and VOC (volatile organic compounds) by using modified fly ash | |
| CN1086959C (en) | Flue gas desulfurizing agent and method | |
| JP4942559B2 (en) | Exhaust gas purifier and method for capturing harmful trace elements | |
| CN1086596C (en) | Exhaust desulfation method | |
| CN1120035C (en) | Flue gas treating process and system | |
| CN101161331A (en) | Method for processing low concentration unwanted waste gas using microwave-solid castoff | |
| CN1234445C (en) | Calcium spraying catalytic desulfurization method in pulverized coal fired boiler and device thereof | |
| CN201791470U (en) | Dry-method suspension bed type flue gas desulfurization system for small and medium sized coal burning boiler | |
| CN111841271A (en) | Flue gas desulfurization and denitrification method and system by utilizing co-treatment of carbon monoxide | |
| CN105642103A (en) | Nano-calcium desulfurizing system | |
| CN110975554A (en) | Method for flue gas desulfurization of lime rotary kiln by using kiln tail ash | |
| CN202620997U (en) | Integrated device for purifying flue gas generated during refuse burning | |
| CN212215114U (en) | Efficient is dry process deacidification device for msw incineration flue gas | |
| CN203724999U (en) | Desulfurization and denitration device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070725 Termination date: 20100509 |