CN101972595A - Method for implementing magnesium-ammonia combined flue gas desulfuration and decarbonization and by-product recovery - Google Patents
Method for implementing magnesium-ammonia combined flue gas desulfuration and decarbonization and by-product recovery Download PDFInfo
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- CN101972595A CN101972595A CN2010105167243A CN201010516724A CN101972595A CN 101972595 A CN101972595 A CN 101972595A CN 2010105167243 A CN2010105167243 A CN 2010105167243A CN 201010516724 A CN201010516724 A CN 201010516724A CN 101972595 A CN101972595 A CN 101972595A
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a method for implementing magnesium-ammonia combined flue gas desulfuration and decarbonization and by-product recovery in the technical field of environment. A method for recycling a desulfurization product of magnesium sulfate through ammonium carbonate/bicarbonate prepared through decarbonization and concentrating ammonium sulfate is utilized, waste liquor subjected to wet magnesium-desulphurization is regenerated on the basis of guaranteeing the desulphurization efficiency, the prepared basic magnesium carbonate solid is used for desulphurization recycling, and simultaneously a by-product of ammonium sulfate solid is prepared. The comprehensive technology for gathering carbon dioxide in the flue gas by using ammonia water so as to produce ammonium carbonate/bicarbonate and treating the magnesium sulfate produced through wet magnesium-desulphurization by using ammonium bicarbonate can simultaneously remove the carbon dioxide in the flue gas and obtain basic magnesium carbonate and ammonium sulfate fertilizers.
Description
Technical field
What the present invention relates to is the method for the desulfurization and decarburization coupling in a kind of Environmental Technology field, the implementation method of particularly a kind of magnesium-ammonia combination smoke desulfurization and decarburization and by-product recovery.
Background technology
China be in the world coal year the consumption maximum country, fire coal is the main energy of China.The coal-fired sulfur dioxide that is produced is very huge, causes acid rain to pollute.Country has explicitly called for industry and coal-fired boiler in power plant must carry out flue gas desulfurization and has handled.
The method that coal-fired flue gas desulfurization is handled has multiple.Wherein commonly used with limestone wet-process, but this method need consume a large amount of lime stones and water, produces a large amount of byproduct calcium sulfate simultaneously and is difficult to handle, so be applied to the coal-burning boiler of large power plant basically.The ammonia process of desulfurization and sea water desulfuration also have application in China, but limitation is respectively arranged.The ammonia process of desulfurization is had relatively high expectations to equipment, and the escape loss of ammonia simultaneously can cause secondary environmental pollution; Sea water desulfuration then mainly is confined to the coastal area and uses, and following simultaneously needs a large amount of Seawater Treatment.
Since 1975, the desulfurization of magnesium method begins to apply in countries such as Japan, the U.S., and progressively ripe and expand to the whole world.Magnesium method desulfur technology has the desulfuration efficiency height, is not easy fouling, the place takies advantages such as little.China is one of most important in the world magnesia producing country, the innate advantage of magnesium method desulfur technology extensive application.Especially under the smaller situation in medium small boiler or desulfurization facility place, the most suitable application of this method.But this method also has shortcoming.In recent years, along with the raw material in the worldwide appreciate, the cost of magnesium method desulfur technology raises gradually.Sweetening process need continue Mg supplementation based raw material (mainly being light-magnesite powder), and it is a lot of that desulphurization cost is increased.For this reason, but the magnesium method sulfur removal technology of exploitation economic recovery and consider collecting carbonic anhydride and the method for utilization has bigger technical advantage.
Summary of the invention
The present invention is directed to the deficiency of existing magnesium method desulfur technology, the implementation method of a kind of magnesium-ammonia combination smoke desulfurization and decarburization and by-product recovery is provided.The present invention can also obtain basic magnesium carbonate and ammonium sulfate fertilizer guaranteeing can to remove the carbon dioxide in the flue gas simultaneously under the smoke desulfurization efficiency prerequisite.
The present invention is achieved by the following technical solutions:
It is as follows to the present invention includes step:
(1) utilizes magnesia or basic magnesium carbonate slurries that flue gas is carried out desulfurization, the doctor solution that contains magnesium sulfite and magnesium bisulfite after the desulfurization is imported in the oxidation pond, add Mg (OH)
2The aqueous solution is neutralized to 7 with pH, further blasts air and agitated liquid then; Solution after the aeration oxidation is carried out mechanical removal of impurities with separation equipment, remove the solid flue dust in the flue gas, obtain Adlerika;
(2) pure Adlerika is squeezed in the regenerated reactor, supplementing water or dilute ammonium sulfate solution dilute sulphuric acid magnesium solution, add a spot of flocculant after, airtight stirring decarburizing reaction 2h～6h under 40 ℃～70 ℃ temperature;
(3) when ammonium sulfate concentrations in the solution surpasses 40%, through after the Separation of Solid and Liquid, obtain the basic magnesium carbonate of solid, liquid phase is an ammonium sulfate;
(4) separate with centrifuge instrument, filtrate leaving standstill separated out ammonia sulfate crystal, collects, and it is recycling that clear liquid is squeezed into oxidation pond, carries concentrated sulfuric acid ammonium simultaneously; The basic magnesium carbonate solid sediment that obtains is dissolved in the water and is prepared into desulfurization slurry, and circulation is used for desulfurization.
Desulfurization described in the step (1), the N-process chemical equation of waste liquid is after the desulfurization:
MgO+H
2O→Mg(OH)
2，
Mg(OH)
2+Mg(HSO
3)
2→2MgSO
3+H
2O。
Aeration oxidation described in the step (1), aeration oxidizing process chemical equation is:
2MgSO
3+O
2→2MgSO
4。
Decarbonizing process chemical equation described in the step (2) is:
NH
3·H
2O+CO
2→NH
4HCO
3。
Decarburization described in the step (2), its absorbent are the ammonia spirit of 5-25%.
Dilute sulphuric acid magnesium solution described in the step (2), the concentration of Adlerika are smaller or equal to 15%, otherwise the solid panel junction phenomena can appear in course of reaction.
Flocculant described in the step (2) is one or more in polyacrylamide, the polyvinyl alcohol, and each cubic metre reaction solution adds 50g, with the magnesium ion mol ratio be that the ratio of 2.0-2.5 progressively adds ammonium bicarbonate soln.
Regenerative process chemical equation described in the step (3) is:
MgSO
4+2NH
4HCO
3→Mg(HCO
3)
2+(NH
4)
2SO
4，
4Mg(HCO
3)
2→3MgCO
3·Mg(OH)
2·xH
2O+5CO
2。
The desulfurization again that is used to circulate of basic magnesium carbonate solid described in the step (3) is used, or makes technical grade basic carbonate magnesium products after the drying.
Ammonium sulfate described in the step (3) then is used for diluting high-concentration desulfurized stoste to be regenerated, and concentrated vitriol ammonium in the regenerative process of magnesium sulfate is by crystallization reclaim sulfuric acid ammonium crystal.
Such flue gas desulfurization of the present invention and the coupling of flue gas decarbonization technology are formed one and are reached desulfurization and the technology that will look for novelty that subtracts carbon simultaneously, select the reaction of ammoniacal liquor or ammonium salt and magnesium sulfate for use, carry out magnesium and reclaim.Otherwise the ammoniacal liquor cost is too high, and course of reaction has the escaping of ammonia, causes new pollution; Select for use other ammonium salt can introduce foreign ion or cost is too high; In the course of reaction that magnesium reclaims, add flocculant, can make reacted Separation of Solid and Liquid process more smooth, help to improve the magnesium recovering effect simultaneously.Through laboratory proofing since with the feature of carbonic hydroammonium chemical reaction, the concentration that is used for the Adlerika that magnesium reclaims can not be too high.
The present invention squeezes into Adlerika in the regenerated reactor, adds flocculant and ammonium bicarbonate soln, and Mg-base desulfurizing agent is carried out regenerative response.Fully after the reaction, obtain the mixed solution of basic magnesium carbonate solid and ammonium sulfate, magnesium sulfate.Basic magnesium carbonate is transported to the desulfuration solution preparation system, is used for circulation desulfurization and utilizes.After the filtrate cooling, can separate out purer ammonia sulfate crystal.Clear liquid is partly squeezed into the aeration tank, and circulation is handled again, collects ammonia sulfate crystal and is used for the fertilizer use.
The present invention utilizes the resulting carbonic acid of decarburization (hydrogen) ammonium that desulfurization product magnesium sulfate is carried out reclaiming and ammonium sulfate is put forward dense method, on the basis that guarantees desulfuration efficiency, waste liquid for the desulfurization of wet type magnesium method is regenerated, the basic magnesium carbonate solid that obtains is used for desulfurization and utilizes, obtains the accessory substance ammonium sulfate solids simultaneously.The present invention utilizes carbon dioxide generating carbonic acid (hydrogen) ammonium in the ammoniacal liquor capture flue gas, the complex art handled of the magnesium sulfate that magnesium method wet type desulfurizing is produced with the carbon ammonium again, the carbon dioxide in the flue gas be can remove simultaneously, basic magnesium carbonate and ammonium sulfate fertilizer obtained simultaneously.
Description of drawings
Fig. 1 is a invention process process flow schematic diagram.
The specific embodiment
Below in conjunction with accompanying drawing embodiments of the invention are elaborated: following examples have provided detailed embodiment and process being to implement under the prerequisite with the technical solution of the present invention, but protection scope of the present invention is not limited to following embodiment.
As shown in Figure 1, following examples are at first carried out flue gas desulfurization with magnesia or basic magnesium carbonate slurries, and the waste liquid after desulfurization adds the magnesia solid, regulator solution pH to 7.0, and aeration oxidation then, the magnesium sulfite in the solution is converted into magnesium sulfate.Carry out Separation of Solid and Liquid with mechanical separation equipment (filter press), remove the solid flue dust in the flue gas, filtrate is purer Adlerika.Then, in regenerated reactor, add entry or dilute ammonium sulfate solution dilute sulphuric acid magnesium solution, make magnesium sulfate concentration be no more than 15%, add a small amount of polyvinyl alcohol (each cubic metre reaction solution adds 50g), with with the magnesium ion mol ratio be that the ratio of 2.0-2.5 progressively adds ammonium bicarbonate soln, airtight stirring reaction 2h～6h under 40 ℃～70 ℃ temperature; Separate with centrifuge, the basic magnesium carbonate Solid Conveying and Melting that obtains is used for circulation desulfurization and uses to the slurrying pond; Separate out ammonia sulfate crystal after the filtrate cooling, collect, it is recycling that supernatant is squeezed into oxidation pond.
Embodiment 1
Present embodiment takes by weighing 262.0g epsom salt solid (containing the magnesium elements amount is 13.47%), is dissolved in the 1500ml water, and configuration contains the solution 1500ml of magnesium sulfate 10%, PH=7.Under 60 ℃ of temperature, metering divides and adds 232.0g carbonic hydroammonium solid for five times, and airtight stirring reaction is 3 hours under 60 ℃ of temperature.Separate with centrifuge, obtain about 280g of basic magnesium carbonate solid (wet, as to be about 80g after 120 ℃ of dryings) and filtrate 1300ml.Detect magnesium ion content in the filtrate with EDTA method (GB/T 15452-95), determine to have in the regenerative response 80% magnesium ion to be converted into the basic carbonate magnesium precipitate through calculating.
Present embodiment is collected the filtrate 1500ml of above-mentioned reaction as solvent, add 262.0g epsom salt solid (containing the magnesium elements amount is 13.47%), under 60 ℃ of temperature, metering divides and adds 232.0g carbonic hydroammonium solid for five times, and airtight stirring reaction is 3 hours under 60 ℃ of temperature.Separate with centrifuge, obtain about 330g of basic magnesium carbonate solid (wet, as to be about 95g after 120 ℃ of dryings) and filtrate 1300ml.Detect magnesium ion content in the filtrate with EDTA method (GB/T 15452-95), determine to have in the regenerative response 80% magnesium ion to be converted into the basic carbonate magnesium precipitate through calculating.
Behind present embodiment two secondary responses, filtrate is separated out the small amount of ammonium sulfate crystal through supercooling, collects back drying under 75 ℃ of temperature, obtains the 5.2g solid.
Embodiment 2
Present embodiment takes by weighing 262.0g epsom salt solid (containing the magnesium elements amount is 13.47%), is dissolved in the 1500ml water, and configuration contains the solution 1500ml of magnesium sulfate 10%, PH=7.Under 60 ℃ of temperature, add the 0.5g polyvinyl alcohol, metering divides and adds 232.0g carbonic hydroammonium solid for five times, and airtight stirring reaction is 3 hours under 60 ℃ of temperature.Separate with centrifuge, obtain about 315g of basic magnesium carbonate solid (wet, as to be about 90g after 120 ℃ of dryings) and filtrate 1300ml.Detect magnesium ion content in the filtrate with EDTA method (GB/T 15452-95), determine to have in the regenerative response 90% magnesium ion to be converted into the basic carbonate magnesium precipitate through calculating.
Present embodiment is collected the filtrate 1500ml of above-mentioned reaction as solvent, add 262.0g epsom salt solid (containing the magnesium elements amount is 13.47%), under 60 ℃ of temperature, add the 0.5g polyvinyl alcohol, metering divides and adds 232.0g carbonic hydroammonium solid for five times, and airtight stirring reaction is 3 hours under 60 ℃ of temperature.Separate with centrifuge, obtain about 340g of basic magnesium carbonate solid (wet, as to be about 100g after 120 ℃ of dryings) and filtrate 1300ml.Detect magnesium ion content in the filtrate with EDTA method (GB/T 15452-95), determine to have in the regenerative response 90% magnesium ion to be converted into the basic carbonate magnesium precipitate through calculating.
Behind present embodiment two secondary responses, filtrate is separated out the small amount of ammonium sulfate crystal through supercooling, collects back drying under 75 ℃ of temperature, obtains the 6.5g solid.
Embodiment 3
Present embodiment takes by weighing the technical grade light calcined magnesia (content of magnesia is 95%) of 35Kg, and solution is prepared into configuration and contains 10% magnesian slurries in 300L water.Liquid-gas ratio 2.5L/m
3, desulfurizing tower diameter 480mm, height 3000mm is provided with two two-layer spray systems and individual layer eddy flow plate in the tower.Desulfurization slurry sprays from top of tower, reversely contacts with flue gas, and fully gas-liquid contacts and reacts on the eddy flow plate, and desulfurization slurry absorbs the sulfur in smoke pernicious gas.The sulfur in smoke removal efficiency is 96%.
Flue gas behind the present embodiment desulfurizing and purifying is gone in the atmosphere through direct smoke stack emission behind the demister, and the part flue gas after being purified enters decarbonizing tower by the pipeline of a diameter 80mm.Decarbonizing tower diameter 250mm, height 2500mm is provided with two-layer packing layer and two-layer spray system in the tower.Decarbonizing tower base diameter 480mm is contained with the ammonia spirit of the concentration 10% of 50L.By the pump circulation ammoniacal liquor is squeezed into top of tower and be sprayed onto packing layer, flue gas contacts in the abundant gas-liquid of packing layer with ammoniacal liquor and reacts, and carbon dioxide in the flue gas and ammoniacal liquor reaction generate carbonic hydroammonium.
The PH of liquid phase stopped desulfurization less than 6.5 o'clock in the present embodiment desulfurization slurry, and the solution behind the aeration oxidation sweetening, aeration oxidization time are 4 hours.Solution behind the extraction 30L aeration is driven in the retort PH=7 after the centrifugal filtration.Under 60 ℃ of temperature, stir adding 4.5g polyvinyl alcohol, divided five minor ticks then 15 minutes, add the ammonium bicarbonate soln of 50L.Confined reaction 3 hours.
The present embodiment reacted solution is filtered with centrifuge, obtains solid (oven dry back quality is 5.9Kg) and the 80L filtrate (PH=8.5) of 17.8Kg.With the magnesium ion content in EDTA method (GB/T 15452-95) the detection filtrate, magnesium ion concentration is 0.10mol/L.Filtrate is separated out ammonia sulfate crystal 0.8Kg through the nature cooling.Filtrate adds the concentrated use of circulation in the desulfurization slurry.
Embodiment 4
Present embodiment takes by weighing the technical grade light calcined magnesia (content of magnesia is 95%) of 30Kg, mixes with the 5.9Kg basic magnesium carbonate that last secondary response obtains, and solution is prepared into desulfurization slurry in 300L water.Liquid-gas ratio 2.5L/m
3, desulfurizing tower diameter 480mm, height 3000mm is provided with two two-layer spray systems and individual layer eddy flow plate in the tower.Desulfurization slurry sprays from top of tower, reversely contacts with flue gas, and fully gas-liquid contacts and reacts on the eddy flow plate, and desulfurization slurry absorbs the sulfur in smoke pernicious gas.The sulfur in smoke removal efficiency is 94%.
Flue gas behind the present embodiment desulfurizing and purifying is gone in the atmosphere through direct smoke stack emission behind the demister, and the part flue gas after being purified enters decarbonizing tower by the pipeline of a diameter 80mm.Decarbonizing tower diameter 250mm, height 2500mm is provided with two-layer packing layer and two-layer spray system in the tower.Decarbonizing tower base diameter 480mm is contained with the ammonia spirit of the concentration 10% of 50L.By the pump circulation ammoniacal liquor is squeezed into top of tower and be sprayed onto packing layer, flue gas contacts in the abundant gas-liquid of packing layer with ammoniacal liquor and reacts, and carbon dioxide in the flue gas and ammoniacal liquor reaction generate carbonic hydroammonium.
The PH of liquid phase stopped desulfurization less than 6.5 o'clock in the present embodiment desulfurization slurry, and the solution behind the aeration oxidation sweetening, aeration oxidization time are 4 hours.The ammonium bicarbonate soln of 50L is driven in the retort, under 70 ℃ of temperature, stirs adding 7g polyacrylamide, divided five minor ticks then 15 minutes, the solution behind the 30L aeration after the adding centrifugal filtration, confined reaction 2 hours.
The present embodiment reacted solution is filtered with centrifuge, obtains solid (oven dry back quality is 6.1Kg) and the 80L filtrate (PH=8.5) of 18.0Kg.With the magnesium ion content in EDTA method (GB/T 15452-95) the detection filtrate, magnesium ion concentration is 0.12mol/L.Filtrate is separated out ammonia sulfate crystal 1.1Kg through the nature cooling.Filtrate adds the concentrated use of circulation in the desulfurization slurry.
Claims (6)
1. the implementation method of magnesium-ammonia combination smoke desulfurization and decarburization and by-product recovery is characterized in that, comprises that step is as follows:
(1) utilizes magnesia or basic magnesium carbonate slurries that flue gas is carried out desulfurization, the doctor solution that contains magnesium sulfite and magnesium bisulfite after the desulfurization is imported in the oxidation pond, add Mg (OH)
2The aqueous solution is neutralized to 7 with pH, further blasts air and agitated liquid then, and the solution after the aeration oxidation is carried out mechanical removal of impurities with separation equipment, removes the solid flue dust in the flue gas, obtains Adlerika;
(2) pure Adlerika is squeezed in the regenerated reactor, supplementing water or dilute ammonium sulfate solution dilute sulphuric acid magnesium solution, add a spot of flocculant after, airtight stirring decarburizing reaction 2h～6h under 40 ℃～70 ℃ temperature;
(3) when ammonium sulfate concentrations in the solution surpasses 40%, through after the Separation of Solid and Liquid, obtain the basic magnesium carbonate of solid, liquid phase is an ammonium sulfate;
(4) separate with centrifuge instrument, filtrate leaving standstill separated out ammonia sulfate crystal, collects, and it is recycling that clear liquid is squeezed into oxidation pond, carries concentrated sulfuric acid ammonium simultaneously; The basic magnesium carbonate solid sediment that obtains is dissolved in the water and is prepared into desulfurization slurry, and circulation is used for desulfurization.
2. the implementation method of magnesium according to claim 1-ammonia combination smoke desulfurization and decarburization and by-product recovery is characterized in that, the decarburization described in the step (2), and its absorbent is the ammonia spirit of 2-25%.
3. the implementation method of magnesium according to claim 1-ammonia combination smoke desulfurization and decarburization and by-product recovery is characterized in that, the dilute sulphuric acid magnesium solution described in the step (2), and the concentration of Adlerika is smaller or equal to 15%.
4. the implementation method of magnesium according to claim 1-ammonia combination smoke desulfurization and decarburization and by-product recovery, it is characterized in that, flocculant described in the step (2) is one or more in polyacrylamide, the polyvinyl alcohol, each cubic metre reaction solution adds 50g, with the magnesium ion mol ratio be that the ratio of 2.0-2.5 progressively adds ammonium bicarbonate soln.
5. the implementation method of magnesium according to claim 1-ammonia combination smoke desulfurization and decarburization and by-product recovery is characterized in that, the desulfurization again that is used to circulate of the basic magnesium carbonate solid described in the step (3) is used, or makes technical grade basic carbonate magnesium products after the drying.
6. the implementation method of magnesium according to claim 1-ammonia combination smoke desulfurization and decarburization and by-product recovery, it is characterized in that, ammonium sulfate described in the step (3) then is used for diluting high-concentration desulfurized stoste to be regenerated, concentrated vitriol ammonium in the regenerative process of magnesium sulfate is by crystallization reclaim sulfuric acid ammonium crystal.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103203174A (en) * | 2013-03-27 | 2013-07-17 | 华北电力大学（保定） | Method for collecting SO2 and CO2 in flue gas from coal-fired power plant and producing chemical products |
| CN105611990A (en) * | 2013-10-07 | 2016-05-25 | 里德系统（澳大利亚）私人有限公司 | Method and apparatus for removing carbon dioxide from flue gas |
| CN107952355A (en) * | 2017-10-17 | 2018-04-24 | 上海交通大学 | It is a kind of that the method for promoting zinc oxide flue gas desulfurization is circulated using aluminum sulfate |
| CN110152488A (en) * | 2019-04-28 | 2019-08-23 | 昆明理工大学 | SO in a kind of dry removal coke oven flue gas2Method |
| CN111439758A (en) * | 2020-03-18 | 2020-07-24 | 宁波上福源环保科技有限公司 | Ammonia-containing waste gas recycling device and method |
| CN114432853A (en) * | 2022-01-27 | 2022-05-06 | 南方电网电力科技股份有限公司 | Energy storage, desulfurization and carbon capture integrated device and method and application |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87101759A (en) * | 1986-01-27 | 1987-09-30 | 陶氏化学公司 | Magnesium, calcium oxide composite |
| CN1155575A (en) * | 1996-09-18 | 1997-07-30 | 梁万阳 | Production of catalytic desulfurizing agent for coal |
| CN101053742A (en) * | 2007-02-13 | 2007-10-17 | 上海交通大学 | Method for using magnesium compound and ammonia to circulate regeneration flue gas desulfurization |
-
2010
- 2010-10-22 CN CN2010105167243A patent/CN101972595A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87101759A (en) * | 1986-01-27 | 1987-09-30 | 陶氏化学公司 | Magnesium, calcium oxide composite |
| CN1155575A (en) * | 1996-09-18 | 1997-07-30 | 梁万阳 | Production of catalytic desulfurizing agent for coal |
| CN101053742A (en) * | 2007-02-13 | 2007-10-17 | 上海交通大学 | Method for using magnesium compound and ammonia to circulate regeneration flue gas desulfurization |
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|---|---|---|---|---|
| CN103203174A (en) * | 2013-03-27 | 2013-07-17 | 华北电力大学（保定） | Method for collecting SO2 and CO2 in flue gas from coal-fired power plant and producing chemical products |
| CN103203174B (en) * | 2013-03-27 | 2016-01-13 | 华北电力大学（保定） | SO in a kind of trapping coal-fired plant flue gas 2and CO 2and the method for production chemical product |
| CN105611990A (en) * | 2013-10-07 | 2016-05-25 | 里德系统（澳大利亚）私人有限公司 | Method and apparatus for removing carbon dioxide from flue gas |
| JP2016540626A (en) * | 2013-10-07 | 2016-12-28 | リード システムズ（オーストラリア） ピーティーワイ エルティーディーＲｅｉｄ Ｓｙｓｔｅｍｓ （Ａｕｓｔｒａｌｉａ） Ｐｔｙ Ｌｔｄ | Method and apparatus for removing carbon dioxide from flue gas |
| EP3038737A4 (en) * | 2013-10-07 | 2017-08-23 | Reid Systems (Australia) Pty Ltd. | Method and apparatus for removing carbon dioxide from flue gas |
| CN107952355A (en) * | 2017-10-17 | 2018-04-24 | 上海交通大学 | It is a kind of that the method for promoting zinc oxide flue gas desulfurization is circulated using aluminum sulfate |
| CN107952355B (en) * | 2017-10-17 | 2021-01-22 | 上海交通大学 | Method for promoting zinc oxide flue gas desulfurization by using aluminum sulfate circulation |
| CN110152488A (en) * | 2019-04-28 | 2019-08-23 | 昆明理工大学 | SO in a kind of dry removal coke oven flue gas2Method |
| CN111439758A (en) * | 2020-03-18 | 2020-07-24 | 宁波上福源环保科技有限公司 | Ammonia-containing waste gas recycling device and method |
| CN111439758B (en) * | 2020-03-18 | 2024-02-23 | 宁波上福源环保科技有限公司 | Ammonia-containing waste gas recycling device and method |
| CN114432853A (en) * | 2022-01-27 | 2022-05-06 | 南方电网电力科技股份有限公司 | Energy storage, desulfurization and carbon capture integrated device and method and application |
| CN114432853B (en) * | 2022-01-27 | 2023-03-24 | 南方电网电力科技股份有限公司 | Energy storage, desulfurization and carbon capture integrated device and method and application |
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Application publication date: 20110216 |