CN1349844A - Circular suspension type semi-dry fume purifier - Google Patents
Circular suspension type semi-dry fume purifier Download PDFInfo
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- CN1349844A CN1349844A CN 00131524 CN00131524A CN1349844A CN 1349844 A CN1349844 A CN 1349844A CN 00131524 CN00131524 CN 00131524 CN 00131524 A CN00131524 A CN 00131524A CN 1349844 A CN1349844 A CN 1349844A
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- slurry
- dust remover
- flue gas
- desulfurization
- atomization nozzle
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- 239000000725 suspension Substances 0.000 title claims description 7
- 239000003517 fume Substances 0.000 title abstract description 4
- 239000002002 slurry Substances 0.000 claims abstract description 28
- 239000000428 dust Substances 0.000 claims abstract description 26
- 238000001694 spray drying Methods 0.000 claims abstract description 14
- 238000009692 water atomization Methods 0.000 claims abstract description 11
- 238000002347 injection Methods 0.000 claims abstract description 3
- 239000007924 injection Substances 0.000 claims abstract description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 40
- 230000023556 desulfurization Effects 0.000 claims description 40
- 239000003546 flue gas Substances 0.000 claims description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 26
- 239000000843 powder Substances 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000000889 atomisation Methods 0.000 claims description 7
- 238000000746 purification Methods 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 6
- 230000029087 digestion Effects 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims 1
- 230000003009 desulfurizing effect Effects 0.000 abstract description 14
- 239000007789 gas Substances 0.000 abstract description 7
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 2
- 238000004140 cleaning Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 19
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 15
- 235000011941 Tilia x europaea Nutrition 0.000 description 15
- 239000004571 lime Substances 0.000 description 15
- 239000007788 liquid Substances 0.000 description 12
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 239000002956 ash Substances 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000007787 solid Substances 0.000 description 9
- 230000002745 absorbent Effects 0.000 description 6
- 239000002250 absorbent Substances 0.000 description 6
- 238000001035 drying Methods 0.000 description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 5
- 239000000920 calcium hydroxide Substances 0.000 description 5
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 229910052925 anhydrite Inorganic materials 0.000 description 4
- 235000011116 calcium hydroxide Nutrition 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000011575 calcium Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012467 final product Substances 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000008267 milk Substances 0.000 description 2
- 210000004080 milk Anatomy 0.000 description 2
- 235000013336 milk Nutrition 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The fume cleaning equipment possesses an inverted spray-drying desulfurizing tower, the lower portion of one end of said desulfurizing tower is equipped with water atomizing nozzle, slurry atomizing nozzle, venturi air-distributing device and ash valve, the other end of the desulfurizing tower is connected with dust remover, the other end of said dust remover is connected with induced fan, and the outlet of bottom of the dust remover is connected with fan and feeding injection pump, and is connected with underside of water atomizing nozzle in lower portion of the desulfurizing tower, the slurry atomizing nozzle is connected with air compressor and sturry metering feeding equipment. Said product is simple in structure, also can remove other harmful gas and heavy metal, etc.
Description
The invention relates to a circular suspension type semi-dry method flue gas purification device.
With the development of industry, SO in China2The emission of (2) has resulted in severe acid rain in many regions, with an average economic loss of over 1000 billion yuan. In order to solve the problem of air pollution, China has established more strict SO2Pollution control laws and regulations in the State Council of the recovery of problems associated with acid rain control and Sulfur dioxide pollution control Zones (State Council No. 199875)]File requirement, national SO in 20002The pollution discharge amount is less than 1600 ten thousand tons, the air quality of direct administration cities and provincial meetings in the 'two control areas' and open cities and key tourism cities reaches the national environmental quality standard, and measures such as limiting the exploitation of high-sulfur coal, developing a desulfurization technology, strengthening a pollution discharge charge collection system and the like are taken.
At present, foreign desulfurization technology is mature, but the price of a desulfurization device is quite high, and the operation cost is very high, so that the large-scale popularization and application cannot be achieved in China. Taking a Lopa Huang power plant as an example, the investment cost of aflue gas desulfurization device is 3 million yuan, and the operation cost of the flue gas desulfurization device per year can reach more than 4000 million yuan, so that the problems that the desulfurization device cannot be built and operated generally exist in China abroad. Compared with wet flue gas desulfurization, semi-dry processes such as spray drying flue gas desulfurization and the like have the advantages of simple system and lower manufacturing cost, and can achieve very high calcium utilization rate and desulfurization efficiency when lime slurry is used as a desulfurizing agent. And the final solid product generated by reliable operation is easy to treat, thereby avoiding the problem of secondary pollution.
The invention aims to provide a circular suspension type semi-dry method flue gas purification device which is simple in structure, low in investment and low in operating cost.
In order to achieve the above object, the present invention adopts the following measures:
the circulating suspension type semi-dry flue gas purification device is provided with an inverted U-shaped spray drying desulfurization tower, a water atomization nozzle, a slurry atomization nozzle, a Venturi air distribution device and an ash valve are sequentially arranged on the lower portion of one end of the desulfurization tower, the other end of the desulfurization tower is connected with one end of a dust remover, the other end of the dust remover is connected with an induced draft fan, an outlet in the bottom of the dust remover is connected with one end of a chain conveyor, the other end of the chain conveyor is connected with a fan and a feeding jet pump and is connected with the lower portion of the water atomization nozzle on the lower portion of the desulfurization tower, a waste material outer discharge port is further arranged on the bottom of the dust remover, the water atomization nozzle is connected.
The invention has the following advantages:
1) simple flow and less equipment. A set of equipment for treating waste liquid, such as a concentrator, a centrifugal machine, a filter and the like, is eliminated. The initial investment is low;
2) the product is easy to process;
3) as long as the temperature of the exhaust gas is proper and no serious corrosion exists, the tail flue and the absorption tower can be made of common steel;
4) a dry temperature interface does not exist, so that the phenomenon of scaling and blockage is eliminated;
5) the operation adaptability is strong, the dosage of the absorbent can be changed along with the inlet SO2The concentration is changed without strictly controlling the pH value as in a wet system.
6) The number of operators and maintenance personnel is small;
7) the energy consumption is low, the energy consumption is about 0.5 percent of the generated energy at first and is only 25-50 percent of that of a wet method, and one reason is that the flue gas is not required to be reheated;
8) the purified flue gas can be directly discharged without being reheated.
9) The operation cost is low, and the water consumption is much lower than that of a wet method;
10) the process is designed by adopting a system integration multi-objective optimization technology, so that the investment is more saved, and the operation is more economical. Since spray dry desulfurization has the above-mentioned advantages, it is inevitably used more and more widely. The process has simple structure, low investment and low operating cost, can remove other harmful gases, even heavy metals and the like, and is very suitable for domestic popularization and application.
The present invention will be described in detail with reference to the accompanying drawings.
The attached drawing is a structural schematic diagram of the invention.
The circulating suspension type semi-dry flue gas purification device is provided with an inverted U-shaped spray drying desulfurization tower 1, the lower part of one end of the desulfurization tower is sequentially provided with a water atomization nozzle 2, a slurry atomization nozzle 5, a Venturi air distribution device 6 and an ash valve 7, the other end of the desulfurization tower is connected with one end of a dust remover 8, the other end of the dust remover is connected with a draught fan 9, the outlet at the bottom of the dust remover is connected with one end of a chain conveyor 10, the other end of the chain conveyor is connected with a fan 12 and a feeding injection pump 11 and is connected with the lower part of the water atomization nozzle at the lower part of the desulfurization tower, the bottom of the dust remover is also provided with a waste material external discharge port 13, the water atomization nozzle is connected with an atomization water pump.
The slurry metering and feeding device is provided with a powder storage bin 14, the powder storage bin is provided with a level meter 20, the bottom of the powder storage bin is sequentially provided with a feeder 15, a digestion conveyor 16 and a slurry pool 18, the upper part of the slurry pool is provided with a stirrer 17 and a supplementing and digesting water pump 21, and the bottom of the slurry pool is provided with a slurry pump 19 and is connected with an air compressor 4 and a slurry atomizingnozzle 5.
Flue gas from the boiler enters the desulfurizing tower from the lower part of the spray drying desulfurizing tower through the Venturi air distribution device. The lime slurry is sprayed from a two-phase flow nozzle at the lower part of the desulfurization tower, mixed with the flue gas and the desulfurization ash from the dust remover in the desulfurization tower at a high mass transfer rate, and mixed with SO in the flue gas2HCl and HF react to produce CaSO4、CaSO3、CaCl2And CaF2And the like. The venturi arrangement not only strengthens the mixing of the flue gas and the absorbent in the tower, can form enough turbulence, but also can effectively prevent the lime slurry from adhering to the wall. This is one of the characteristics of the system different from the traditional spray drying flue gas desulfurization. The large area of intimate contact ensures that the absorbent and SO2With almost instantaneous high efficiency, and the capacity of the reactor is therefore kept to a minimum. The distribution of flue gas, the feeding rate and distribution of the recirculated ash and the amount of make-up water are effectively controlledTo ensure the reduction conditions required to achieve optimum desulfurization efficiency. The dry desulfurization reaction product is prepared fromThe desulfurizing tower enters a bag-type dust remover connected with the desulfurizing tower. One part of the dry ash collected from the dust remover is sent back to the desulfurizing tower for recycling, and the other part of the discharged ash equivalent to the feeding amount of the lime powder is sent to a fly ash storage yard. The system adopts a two-fluid atomizing nozzle, so that the atomizing granularity and the atomizing quality can be well controlled. Compared with a rotary atomizing nozzle, the two-fluid atomizing nozzle is simple in design, and a single nozzle can be operated independently and can be maintained online. The special atomizing nozzle for the process is very firm and wear-resistant and is not blocked. The spray drying process developed by Zhejiang university is different from the traditional spray drying process, and the second characteristic is that: the desulfurized ash residue is recycled and directly enters a spray drying flue gas desulfurization tower instead of a lime pulping system. Therefore, the circulation multiplying power is large, and the lime is more fully utilized. Under the same Ca/S condition, the desulfurization efficiency is higher.
The invention generally uses lime as an absorbent, and also can use slaked lime or other materials containing alkalinity, such as carbide slag, waste lye and the like. The lime powder is transported to the factory by a sealing tank car for a powder mill outside the factory and is positively conveyed to a powder storage bin by compressed air, and the powder storage bin is of a steel structure and is arranged in a nearby open space. The lower part of the powder storage bin is provided with fluidized bottom air to prevent limestone powder from bridging, and the compressed air of the fluidized bottom air comes from an air compressor.
The slurry metering and feeding device consists of a powder storage bin, a feeding hopper, a star-shaped feeder, a screw conveyor and valves. The star-shaped feeder delivers the powder in the powder storage bin to a feeding hopper, the powder is delivered to a digestion tank by a conveyor after being metered by the feeding hopper for digestion, a vibrating screen is used for separating and discarding large particles, and finally the lime milk flows into a lime milk pool and is diluted by adding water.
The intermittent pulp benefiting method is adopted, the slaking process of the quicklime is controlled by adjusting parameters such as water adding quantity, slaking temperature, time and the like, and a slag dischargingport is arranged at the bottom of the slaking tank to discharge the slag.
A bag type dust collector is adopted. Compared with electric dust removal, the bag type dust collector has the following advantages: the unreacted lime deposited on the bag can react with the residual sulfur dioxide in the flue gas, and the desulfurization rate can reach 20 percent of the total desulfurization rate of the system. The filter bag can be regarded as a fixed desulfurizing tower because the flue gas must pass through the dust layer on the filter bag. The bag house dust collector has good effect when being used in a spray drying FGD system. The pressure reduction of the bag-type dust collector as the tail equipment of the spray drying desulfurization system is basically the same as that of the dust collection alone.
Part of the ash collected from the bottom of the reaction tower and the dust collector is returned to the desulfurization tower by the venturi nozzle. The benefits of ash recycling are:
1) the final product contains fly ash generated by coal combustion, is generally alkaline and can be utilized;
2) the final product contains the calcium hydroxide left in the reaction and can also be utilized;
3) the solid particles in the final product play a role of atomizing and dripping cores in the slurry atomization process, so that the specific surface area of the fresh slurry is increased, and according to the chemical reaction kinetics principle, the reaction speed is increased when the specific surface area is increased.
Therefore, the system can directly reduce the consumption of fresh lime. The combination of the three factors can greatly reduce the consumption of the reactant under the condition that the desulfurization efficiency is kept unchanged, and can reduce about 30 percent under the conditionof low sulfur.
The alarm of start-stop operation and abnormal working condition is based on the temperature and SO of the flue gas2The concentration, the flue gas flow and the required desulfurization efficiency are controlled and optimized in the desulfurization process.
The first control loop manages the measurement of the temperature of the inlet and outlet flue gases and the measurement of the flow of the inlet gas, ensuring that the flue gases are cooled to the appropriate temperature for the chemical reaction process to reach the optimum state.
The second control loop is to control the addition of lime, which is achieved by monitoring the inlet flue gas flow and the acid oxide content of the outlet gas, these parameters being constantly monitored by the control system and used to calculate the lime make-up ratio.
And the third control loop continuously controls the circulating amount of the desulfurization ash to the reactor according to the monitored flue gas amount.
The invention uses the principle of spray drying to achieve the purpose of removing the flue gasThe purpose of the sulfur is. SO in flue gas2The removal of (a) is carried out in a spray-drying desulfurization tower, and the chemical and physical processes thereof are as follows.
Chemical reaction process
When the atomized slurry contacts with fume in desulfurizing tower, the absorbent is evaporated, the fume is cooled and humidified, and the lime slurry and SO2The reaction generates a dry powder product, the whole reaction is divided into three states of gas phase, liquid phase and solid phase, and the reaction steps and the agenda formula are as follows:
1)SO2is absorbed by the liquid drop
2) Absorbed SO2Reacting with absorbent in solution to generate calcium sulfite
3) CaSO in liquid droplets3After saturation, crystallization begins
CaSO3(liquid) ═ CaSO3(solid)
4) CaSO in partial solution3Reacts with oxygen dissolved in the liquid drops and is oxidized into calcium sulfate
5)CaSO4Low (liquid) solubility, and thus, crystal precipitation
CaSO4(liquid) ═ CaSO4＝(solid)
6) As the dissolved calcium hydroxide is consumed during desulfurization, more calcium hydroxide solids are further dissolved to maintain the sulfur dioxide removal reaction to continue.
Ca(OH)2(solid) ═ Ca (OH)2(liquid)
Physical process
The physical process refers to the evaporation drying of liquid drops and the cooling and humidifying process of flue gas, and the time required by the liquid drops from the evaporation to the drying is very important for the design of the desulfurizing tower and the desulfurizing rate. Factors that affect drop drying are drop size, drop moisture content, and temperature value toward adiabatic saturation. The drying of the droplets is roughly divided into two stages: the first stage is basically free evaporation of water on the surface of the slurry liquid drop due to the fact that the solid content in the slurry liquid drop is not large, and the evaporation speed is high and relatively constant. As the water evaporates, the solids content of the droplets increases and the second stage is entered when significant solid material is present on the surface of the droplets. As the evaporation surface area becomes smaller, moisture must diffuse through the solid matter from the interior of the particle out, the drying rate decreases, the temperature of the droplet rises and approaches the temperature of the flue gas and eventually separates from the flue gas as solid particles are formed as the water therein evaporates off.
Claims (2)
1. A circulating suspension type semi-dry flue gas purification device is characterized by comprising an inverted U-shaped spray drying desulfurization tower [1], wherein the lower part of one end of the desulfurization tower is sequentially provided with a water atomization nozzle [2], a slurry atomization nozzle [5], a Venturi air distribution device [6]and an ash valve [7], the other end of the desulfurization tower is connected with one end of a dust remover [8], the other end of the dust remover is connected with a draught fan [9], the bottom outlet of the dust remover is connected with one end of a chain conveyor [10], the other end of the chain conveyor is connected with a fan [12]and a feeding injection pump [11]and is connected with the lower part of the water atomization nozzle at the lower part of the desulfurization tower, the bottom of the dust remover is also provided with a waste material external discharge port [13], the water atomization nozzle is connected with an atomization water pump [3], and the slurry atomization nozzle.
2. The circularly suspended semi-dry flue gas purification device as claimed in claim 1, wherein the slurry metering and feeding device comprises a powder storage bin [14]provided with a level gauge [20], the bottom of the powder storage bin is sequentially provided with a feeder [15], a digestion conveyor [16]and a slurry tank [18], the upper part of the slurry tank is provided with a stirrer [17]and a supplement and digestion water pump [21], and the bottom of the slurry tank is provided with a slurry pump [19]and is connected with an air compressor [4]and a slurry atomizing nozzle [5].
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001315242A CN1185041C (en) | 2000-10-24 | 2000-10-24 | Circular suspension type semi-dry fume purifier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001315242A CN1185041C (en) | 2000-10-24 | 2000-10-24 | Circular suspension type semi-dry fume purifier |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1349844A true CN1349844A (en) | 2002-05-22 |
| CN1185041C CN1185041C (en) | 2005-01-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001315242A Expired - Lifetime CN1185041C (en) | 2000-10-24 | 2000-10-24 | Circular suspension type semi-dry fume purifier |
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| Country | Link |
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| CN (1) | CN1185041C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100422643C (en) * | 2006-06-23 | 2008-10-01 | 杭州新世纪能源环保工程股份有限公司 | Smoke purifier of domestic refuse incinerator |
| CN100464825C (en) * | 2006-12-27 | 2009-03-04 | 吉林安洁环保有限公司 | Semi-dry desulfurizing process in double feedback circular fluidized bed |
| CN102085451A (en) * | 2010-12-17 | 2011-06-08 | 秦皇岛双轮环保科技有限公司 | Desulfuration and dust collection method based on reverse spray type semidry method for flue gas of sintering machine |
| CN101279183B (en) * | 2008-05-21 | 2011-11-30 | 大连理工大学 | Spray absorbing and drying-dry powder activating large multiplying power circulating flue gas desulfurization process |
| CN103480272A (en) * | 2013-10-01 | 2014-01-01 | 王脯胜 | Dust-removing, denitration and desulfurization process and device for flue gas of glass kiln |
| CN103977664A (en) * | 2014-05-16 | 2014-08-13 | 山西清泽环境科技有限公司 | Flue gas desulfurization, denitration and dust removal method |
| CN104607628A (en) * | 2015-02-10 | 2015-05-13 | 大英德创精工设备有限公司 | Automatic slag removing system and method for lead melting furnace |
| CN105854501A (en) * | 2016-04-28 | 2016-08-17 | 安徽工业大学 | Emission reduction system for fine particles in sintering process of iron ore |
-
2000
- 2000-10-24 CN CNB001315242A patent/CN1185041C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100422643C (en) * | 2006-06-23 | 2008-10-01 | 杭州新世纪能源环保工程股份有限公司 | Smoke purifier of domestic refuse incinerator |
| CN100464825C (en) * | 2006-12-27 | 2009-03-04 | 吉林安洁环保有限公司 | Semi-dry desulfurizing process in double feedback circular fluidized bed |
| CN101279183B (en) * | 2008-05-21 | 2011-11-30 | 大连理工大学 | Spray absorbing and drying-dry powder activating large multiplying power circulating flue gas desulfurization process |
| CN102085451A (en) * | 2010-12-17 | 2011-06-08 | 秦皇岛双轮环保科技有限公司 | Desulfuration and dust collection method based on reverse spray type semidry method for flue gas of sintering machine |
| CN102085451B (en) * | 2010-12-17 | 2013-04-17 | 秦皇岛双轮环保科技有限公司 | Desulfuration and dust collection method based on reverse spray type semidry method for flue gas of sintering machine |
| CN103480272A (en) * | 2013-10-01 | 2014-01-01 | 王脯胜 | Dust-removing, denitration and desulfurization process and device for flue gas of glass kiln |
| CN103977664A (en) * | 2014-05-16 | 2014-08-13 | 山西清泽环境科技有限公司 | Flue gas desulfurization, denitration and dust removal method |
| CN104607628A (en) * | 2015-02-10 | 2015-05-13 | 大英德创精工设备有限公司 | Automatic slag removing system and method for lead melting furnace |
| CN105854501A (en) * | 2016-04-28 | 2016-08-17 | 安徽工业大学 | Emission reduction system for fine particles in sintering process of iron ore |
| CN105854501B (en) * | 2016-04-28 | 2018-02-02 | 安徽工业大学 | A kind of emission-reducing system of Ore Sintering Process fine particle |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1185041C (en) | 2005-01-19 |
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