CN1245245C - Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method - Google Patents
Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method Download PDFInfo
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- CN1245245C CN1245245C CN 200410024719 CN200410024719A CN1245245C CN 1245245 C CN1245245 C CN 1245245C CN 200410024719 CN200410024719 CN 200410024719 CN 200410024719 A CN200410024719 A CN 200410024719A CN 1245245 C CN1245245 C CN 1245245C
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- liquid
- regeneration
- desulfurizing
- induced crystallization
- flue gas
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 34
- 230000008025 crystallization Effects 0.000 title claims abstract description 34
- 239000000428 dust Substances 0.000 title claims abstract description 26
- 239000002002 slurry Substances 0.000 title claims abstract description 18
- 239000003513 alkali Substances 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title abstract description 16
- 230000008569 process Effects 0.000 title abstract description 11
- 230000006698 induction Effects 0.000 title abstract 2
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 230000008929 regeneration Effects 0.000 claims abstract description 23
- 238000011069 regeneration method Methods 0.000 claims abstract description 23
- 239000006096 absorbing agent Substances 0.000 claims abstract description 22
- 239000013078 crystal Substances 0.000 claims abstract description 14
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 7
- 235000019738 Limestone Nutrition 0.000 claims abstract description 6
- 239000006028 limestone Substances 0.000 claims abstract description 6
- 239000013049 sediment Substances 0.000 claims abstract description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 5
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 5
- 239000004571 lime Substances 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 43
- 239000003546 flue gas Substances 0.000 claims description 43
- 238000006477 desulfuration reaction Methods 0.000 claims description 34
- 238000005516 engineering process Methods 0.000 claims description 17
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 12
- 238000004062 sedimentation Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 8
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 150000003839 salts Chemical class 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 5
- 239000011593 sulfur Substances 0.000 claims description 5
- 229910052717 sulfur Inorganic materials 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000000247 postprecipitation Methods 0.000 claims description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 14
- 230000003009 desulfurizing effect Effects 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000003517 fume Substances 0.000 abstract 4
- 230000023556 desulfurization Effects 0.000 description 15
- 239000011575 calcium Substances 0.000 description 9
- 239000011734 sodium Substances 0.000 description 9
- 230000008676 import Effects 0.000 description 8
- 239000010440 gypsum Substances 0.000 description 5
- 229910052602 gypsum Inorganic materials 0.000 description 5
- 230000001939 inductive effect Effects 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000004480 active ingredient Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical class [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 230000004087 circulation Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000002277 temperature effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The present invention provides a fume desulfurizing and dust collecting induction and crystallization process for circulating utilization by a concentrated slurry double-alkali method. Desulfurizing liquid is inputted to a desulfurizing absorber to generate convection with fume to be treated so that sulfur dioxide and dust in the fume absorbed and adsorbed, the fume is discharged after being purified, one part of discharge liquid at the bottom flows back to the desulfurizing liquid again, and the other part is sent into a crystallizing tank; crystal seeds are added in the crystallizing tank under the condition of stirring to carry out induced crystallization, most of slurry is transferred into a regeneration groove after induced crystallization, and small part of slurry is transferred into a settling pool; settled clear liquid in the settling pool is transferred into the regeneration groove, and then sediment is discharged; the slurry in the regeneration groove is added with lime / limestone for regeneration and is replenished with soda as required, the pH of the regenerated desulfurizing liquid is enhanced to 5.0 to 13.0, the concentration of Na is less than 1.0 mol/l, the concentration of Ca is less than 2000 ppm, and the desulfurizing liquid is outputted to the desulfurizing absorber through a circulating pump for circulating use. The present invention has the advantages of stable running, easy operation, little investment and low running cost.
Description
Technical field
The invention belongs to the Environmental Technology field, relate to a kind of treatment process of flue gas, especially relate to a kind of Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology that is used in particular for eliminating the smoke pollution that combustion of fossil fuels produces.
Background technology
Along with the raising of people to sulfur dioxide and dust pollution understanding, some places have come into effect strict emission control standards, not only require the original discharge concentration of the sulfur dioxide of flue gas to be lower than 650mg/Nm
3, and require sulfur dioxide in flue gas content after treatment must be lower than 150mg/Nm
3, dust must be lower than 50mg/Nm
3In this case, dry type desulfurizing and dust arrester often can't realize or operation, investment cost high.
Double alkali method desulfurizing technology is often adopted by middle-size and small-size system in the common at present employing wet method sulphur removing and dust removing technology.Double alkali method desulfurizing technology is that first alkaline clear liquid with solubility absorbs SO as absorbent in king-tower
2, at tower external application milk of lime or lime absorption liquid is regenerated then.But CaSO very easily appears in reasons such as impurity stripping in oxygen content height, the dust, gas-liquid full contact in the flue gas that (as the burning low-sulfur coal time) produces because under some operating mode in actual motion
4Supersaturation, might cause the loss of devulcanizer and pipeline crystallization obstruction or sodium salt big, have a strong impact on the energy consumption of system and reliable and stable operation cycle.
Summary of the invention
The invention provides a kind of Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology, this technology is stable, easy and simple to handle, small investment, operating cost are low.
Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology of the present invention is:
Doctor solution is imported desulfuration absorber and pending smoke convection absorption absorption sulfur in smoke and dust, discharge after the gas cleaning, the desulfuration absorber bottom is discharged a liquid part and is back to again in the doctor solution, and another part is sent into crystallizing tank; Add crystal seed and carry out induced crystallization in crystallizing tank under condition of stirring, the most of slurries behind the induced crystallization change in the regeneration tank, and the fraction slurries change sedimentation basin over to; The clear liquid that carries out post precipitation in the sedimentation basin changes in the regeneration tank, and sediment is discharged; Add lime or lime stone regeneration in the regeneration tank in the slurries, and replenish soda as required, make the doctor solution pH value after the regeneration be increased to 5.0-13.0, Na
+Concentration is less than 1.0 mol, Ca
2+Concentration is less than 2000ppm, outputs in the desulfuration absorber by circulating pump to recycle.
Described desulfuration absorber bottom is discharged liquid and can most ofly be refluxed, and the amount that generally is back to desulfuration absorber accounts for the reflux ratio of total discharge rate more than or equal to 60%.
The crystal seed that adds in the described crystallizing tank is: a kind of or several can induce CaSO
4Form CaSO
42H
2The oxide of O crystallization or salt, as be selected from SiO
2, CaCl
2, CaSO
3, CaSO
4, BaSO
4In a kind of or several mixture.
In desulfuration absorber, doctor solution is with after pending flue gas contacts, mixes, the SO in the flue gas
2Be desulfurized liquid absorption or absorption, active ingredient Na in the doctor solution with remaining dust
2SO
3And CaSO
3With the SO in the flue gas
2Reactive moieties or all be converted into NaHSO
3And Ca (HSO
3)
2, simultaneously owing to contain SO in the flue gas
3And O
2, there is oxidation reaction in the sweetening process simultaneously, make to draw and contain the oversaturated calcium sulfate of part (gypsum) in the tower doctor solution.The main chemical reactions formula has:
A discharge liquid part of coming out from desulfuration absorber enters backflow, and another part enters in the crystallizing tank, under the stirring at normal temperature effect, carries out the induced crystallization of gypsum, makes the CaSO that is dissolved in the doctor solution
4With CaSO
42H
2The form of O crystallizes out, and most of crystalline solid slurries enter regeneration tank, and small part crystalline solid slurries enter that sedimentation basin is isolated deslagging behind the sediment, the clear liquid retrieval system is used.
When selecting crystal seed during the induced crystallization of gypsum,, in general, can induce the material of acceleration crystallization to mainly contain following a few class: (1) and CaSO by the own characteristics of crystallization among the conventional theoretical and the present invention of crystallization
42H
2Akin oxide of O crystalline structure or salt; (2) and CaSO
42H
2Akin oxide of O surface charge state or salt; (3) and CaSO
42H
2Akin oxide of O crystallization mechanism or salt.And among the present invention, the oxide or the salt that meet above 3 close crystallization principles have SiO
2, CaCl
2, CaSO
3, CaSO
4, BaSO
4Deng, specifically can be selected wherein a kind of or several mixture by the different situations of the content of pending sulfur dioxide in flue gas and other pernicious gases.
The clear liquid that returns slurries from crystallizing tank and the sedimentation basin carries out neutralization reaction with the soda lime or the lime stone that add in regeneration tank, replenish a part of soda simultaneously as required, the pH value is raise, make it recover high desulfurization activity, and reenter absorption absorption in the devulcanizer.Main chemical reactions in regeneration tank has:
Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology of the present invention has been inherited the advantage of two alkaline process, avoided the interference of high oxidation rate simultaneously to two alkaline process, can blocking pipe and absorber in desulfurization and in as the flow process of afterbody dedusting, the utilization rate height of soda is discharged the most of directly backflow of liquid, and capacity of returns is big, water loss is few, the sedimentation basin volume is little, and desulfurization and dedusting operating cost is low, and desulfurization and dedusting is respond well.
Description of drawings
Fig. 1 is a process chart of the present invention.
The specific embodiment
Technology of the present invention is made up of desulfurization and dedusting part, induced crystallization part, pH recovered part three parts, and is specific as follows:
1. desulfurization and dedusting part
Flue gas after dry type or wet dust removal in desulfuration absorber with contain Na2SO
3And CaSO
3The mixed liquor of active ingredient fully contacts, mixes fully, makes sulfur in smoke and dust be desulfurized liquid absorption or absorption, and the flue gas after desulfurization and the dedusting discharges after demister is removed steam again.The liquid that absorbs and adsorbed sulfur dioxide and dust is discharged from the bottom.Discharge the liquid major part and be back in the desulfuration absorber, fraction is sent into crystallizing tank.
2. crystalline portion
The discharge liquid that partially absorbs and adsorbed sulfur dioxide and dust is sent in the crystallizing tank, under agitation add crystal seed and carry out induced crystallization, fraction high concentration slurries enter sedimentation basin after the crystallization, and the most of slurries of crystallizing tank and the clear liquid of sedimentation basin change regeneration tank over to, and sediment carries out regular deslagging.
3.pH recovered part
The clear liquid pH value that changes regeneration tank over to is lower, adds lime or lime stone and regenerates, and the pH value is raise, and recovers high desulphurizing ability, reenters desulfuration absorber and recycles, and the doctor solution pH value that enters desulfuration absorber is controlled at 5.0-13.0, Na
+Concentration is less than 1.0 mol, Ca
2+Concentration is less than 2000ppm.
Concrete technology as shown in Figure 1, dual alkali scrubbing FGD process induced crystallization utilization process is recovered three parts by desulfurization and dedusting, induced crystallization and pH and is formed; Desulfuration absorber 1 can adopt plate columns such as rotating stream tray scrubber, sieve-plate tower, bubble column and packed tower, venturi, spray column etc., desulfurization, dedusting and demist are carried out in same tower, utilize the kinetic energy of gas that doctor solution is atomized, make gas-liquid fully contact, mix, sulfur in smoke and remaining dust are desulfurized liquid absorption or absorption, active ingredient Na in the doctor solution
2SO
3And CaSO
3With the SO in the flue gas
2Reactive moieties or all be converted into NaHSO
3And Ca (HSO
3)
2, simultaneously owing to contain SO in the flue gas
3And O
2, there is oxidation reaction in the sweetening process simultaneously, make to draw and contain the oversaturated calcium sulfate of part (gypsum) in the tower doctor solution.
The discharge liquid that comes out from devulcanizer all enters in the crystallizing tank 2, adds the induced crystallization that crystal seed carries out gypsum under stirring action, makes the CaSO that is dissolved in the doctor solution
4With CaSO
42H
2The form of O crystallizes out, temperature normal temperature, this moment pH value 3.0-10, after certain hour hour was carried out in crystallization, fraction entered sedimentation basin 3 and isolates sediment, most of slurries enter regeneration tank 4.
The clear liquid that returns from the slurries of crystallizing tank 2 and sedimentation basin in regeneration tank 4 and the soda lime or the lime stone of adding carry out neutralization reaction, the pH value is raise, and adding replenishes alkali, additional alkali is soda ash, caustic soda or salkali waste, make doctor solution recover its high desulfurization activity again, enter to absorb in the desulfuration absorber 1 by circulating pump 5 circulations and adsorb SO
2And dust.
In flue-gas temperature is 150 ℃, import flue gas SO
2Concentration is 2000mg/m
3, the described pH that enters the doctor solution (being in the regeneration tank) of devulcanizer is 9.0, Na
+Concentration is 0.02 mol, Ca
2+Concentration is 20ppm, with the liquid-gas ratio L/G of flue gas be 3.0L/m
3
The amount that bottom discharge liquid is back to desulfuration absorber accounts for the percentage of discharging the liquid total amount, and promptly reflux ratio is 95%.
The pH value is controlled at 8.0 in the described crystallizing tank, and inducing crystal seed is an amount of SiO
2, CaSO
3, CaSO
4Mixture.
After the whole system operation, described smoke desulfurization efficiency reaches 90%.
In flue-gas temperature is 150 ℃, import flue gas SO
2Concentration is 2000mg/m
3, the described pH that enters the doctor solution (being in the regeneration tank) of devulcanizer is 8.0, Na
+Concentration is 0.01 mol, Ca
2+Concentration is 20ppm, with the liquid-gas ratio L/G of flue gas be 3.0L/m
3, reflux ratio is 85%.
The pH value is controlled at 7.0 in the described crystallizing tank, and inducing crystal seed is an amount of SiO
2
After the whole system operation, described smoke desulfurization efficiency reaches 85%.
In flue-gas temperature is 150 ℃, import flue gas SO
2Concentration is 500mg/m
3, be 120 ℃ in flue-gas temperature, import flue gas SO
2Concentration is 500mg/m
3, the described pH that enters the doctor solution of devulcanizer is 12.0, Na
+Concentration is 0.4 mol, Ca
2+Concentration is 1000ppm, with the liquid-gas ratio L/G of flue gas be 15.0L/m
3, reflux ratio is 90%.
The pH value is controlled at 10.0 in the described crystallizing tank, and inducing crystal seed is an amount of SiO
2, CaCl
2, CaSO
3, CaSO
4, BaSO
4Mixture.
After the whole system operation, described smoke desulfurization efficiency reaches 99%.
In flue-gas temperature is 150 ℃, import flue gas SO
2Concentration is 500mg/m
3, be 130 ℃ in flue-gas temperature, import flue gas SO
2Concentration is 500mg/m
3, the described pH that enters the doctor solution of devulcanizer is 9.0, Na
+Concentration is 0.6 mol, Ca
2+Concentration is 100ppm, with the liquid-gas ratio L/G of flue gas be 15.0L/m
3, reflux ratio is 70%.
The pH value is controlled at 6.0 in the described crystallizing tank, and inducing crystal seed is proper C aCl
2, CaSO
3, CaSO
4Mixture.
After the whole system operation, described smoke desulfurization efficiency reaches 80%.
In flue-gas temperature is 150 ℃, import flue gas SO
2Concentration is 4000mg/m
3, be 140 ℃ in flue-gas temperature, import flue gas SO
2Concentration is 500mg/m
3, the described pH that enters the doctor solution of devulcanizer is 7.0, Na
+Concentration is 0.06 mol, Ca
2+Concentration is 400ppm, with the liquid-gas ratio L/G of flue gas be 1.0L/m
3, reflux ratio is 80%.
The pH value is controlled at 5.0 in the crystallizing tank, and inducing crystal seed is an amount of SiO
2, CaCl
2, CaSO
3, CaSO
4Mixture.
After the whole system operation, described smoke desulfurization efficiency reaches 70%.
Claims (4)
1. a Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology is:
Doctor solution is imported desulfuration absorber and pending smoke convection absorption absorption sulfur in smoke and dust, discharge after the gas cleaning, the desulfuration absorber bottom is discharged a liquid part and is back to again in the doctor solution, and another part is sent into crystallizing tank; Add crystal seed and carry out induced crystallization in crystallizing tank under condition of stirring, the most of slurries behind the induced crystallization change in the regeneration tank, and the fraction slurries change sedimentation basin over to; The clear liquid that carries out post precipitation in the sedimentation basin changes in the regeneration tank, and sediment is discharged; Add lime or lime stone regeneration in the regeneration tank in the slurries, and replenish soda as required, make the doctor solution pH value after the regeneration be increased to 5.0-13.0, Na
+Concentration is less than 1.0 mol, Ca
2+Concentration is less than 2000ppm, outputs in the desulfuration absorber by circulating pump to recycle.
2. Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology according to claim 1 is characterized in that: the amount that described desulfuration absorber bottom discharge liquid is back to desulfuration absorber accounts for the reflux ratio of total discharge rate more than or equal to 60%.
3. Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology according to claim 1 is characterized in that: the crystal seed that adds in the described crystallizing tank is: a kind of or several can induce CaSO
4Form CaSO
42H
2The oxide of O crystallization or salt.
4. Dual-alkali flue gas desulphurization dust removaling induced crystallization recycling technology according to claim 3 is characterized in that: the crystal seed that adds in the described crystallizing tank is: be selected from SiO
2, CaCl
2, CaSO
3, CaSO
4, BaSO
4In a kind of or several mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410024719 CN1245245C (en) | 2004-05-25 | 2004-05-25 | Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410024719 CN1245245C (en) | 2004-05-25 | 2004-05-25 | Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1583230A CN1583230A (en) | 2005-02-23 |
| CN1245245C true CN1245245C (en) | 2006-03-15 |
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ID=34600966
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410024719 Expired - Fee Related CN1245245C (en) | 2004-05-25 | 2004-05-25 | Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method |
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100435910C (en) * | 2006-04-10 | 2008-11-26 | 广州市天赐三和环保工程有限公司 | Fume desulfurizing process employing multiple circulation and stable double alkali method and apparatus |
| CN101816887A (en) * | 2010-05-07 | 2010-09-01 | 吉林安洁环保有限公司 | High-alkaline double-alkali simplified desulfuration control method by adding agent at front end of canal |
| CN102085450B (en) * | 2010-12-17 | 2013-05-29 | 秦皇岛双轮环保科技有限公司 | Integrated desulfuration and dust removal method for medium and small boiler flue gas |
| CN102166470A (en) * | 2011-03-09 | 2011-08-31 | 西安西矿环保科技有限公司 | Dual-alkali smoke desulfurization device and desulfurization method thereof |
| CN102485323A (en) * | 2011-04-15 | 2012-06-06 | 安徽理工大学 | Rapid calcium desulphurization method for flue gas |
| CN103920396B (en) * | 2014-03-31 | 2015-11-25 | 煤科集团杭州环保研究院有限公司 | A kind of open type double alkali method desulfurizing gypsum autoxidation system and control method thereof |
| CN105585177A (en) * | 2016-02-05 | 2016-05-18 | 大唐环境产业集团股份有限公司 | Desulfurization wastewater softening device and method |
| CN106904711A (en) * | 2017-04-20 | 2017-06-30 | 盐城工学院 | A kind of calcium carbonate waste water circulation recovery system and calcium carbonate circulating purification system |
| CN110302641A (en) * | 2019-04-25 | 2019-10-08 | 太仓北新建材有限公司 | A kind of desulfurizer and sulfur removal technology of flue gas |
| CN112755784A (en) * | 2020-12-21 | 2021-05-07 | 通化金山银山环保设备制造有限公司 | Method for removing sodium sulfate in boiler dual-alkali desulfurization process |
| CN115159555B (en) * | 2022-08-01 | 2023-12-22 | 华中科技大学 | Method and system for treating solid waste incineration flue gas |
-
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- 2004-05-25 CN CN 200410024719 patent/CN1245245C/en not_active Expired - Fee Related
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| Publication number | Publication date |
|---|---|
| CN1583230A (en) | 2005-02-23 |
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