CN111729474B - Method for circulating flue gas desulfurization and sulfur dioxide recovery by using organic acid magnesium solution - Google Patents
Method for circulating flue gas desulfurization and sulfur dioxide recovery by using organic acid magnesium solution Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2258/0283—Flue gases
Abstract
The invention belongs to the field of environmental protection, relates to a method for recycling flue gas desulfurization and sulfur dioxide by using an organic magnesium solution, and provides a method for realizing efficient capture, desorption and recovery of sulfur dioxide and conveniently removing sulfate in the solution by using the organic magnesium solution to replace a conventional recyclable desulfurizer. The method comprises the following steps: preparing an organic magnesium solution, absorbing sulfur dioxide in flue gas, desorbing sulfur dioxide in a rich solution, recycling a regenerated barren solution, removing sulfate radicals and the like. The organic magnesium sulfate solution has excellent buffering effect on the absorption process of sulfur dioxide, large absorption capacity, low desorption and regeneration temperature and easy removal of sulfate by-products. Compared with the prior art, the desulfurizer disclosed by the invention is low in cost, good in desulfurization effect and has a denitration function. In addition, the desulfurizer has the characteristics of environmental friendliness, no secondary pollution and the like, and is particularly suitable for recycling sulfur dioxide in industrial flue gas in the fields of energy, metallurgy, chemical industry and the like.
Description
Technical Field
The invention belongs to the field of environmental protection, mainly aims at the treatment of sulfur dioxide in flue gas, and relates to a method for flue gas desulfurization and sulfur dioxide recovery.
Background
With the continuous improvement of the environmental standard of China, the treatment technology for various pollutants is continuously updated. The removal of sulfur dioxide in flue gas discharged by industry is always a key problem, and the removal, recovery and resource utilization of sulfur dioxide in the fields of energy, metallurgy and chemical industry are always concerned. The sulfur dioxide output in the energy production industry is larger, a wet desulphurization process is generally adopted, the removal efficiency is higher and stable at present, the desulphurization by-product can also be recycled, but in the industries of nonferrous smelting, petrifaction and the like, sulfur-containing flue gas with different concentrations can be generated in different process sections. When the concentration of sulfur dioxide in the flue gas is more than 4%, a contact type acid making process can be generally adopted to produce sulfuric acid; when the concentration of sulfur dioxide in the flue gas is below 1%, a desulfurization method of discarding desulfurization products is often adopted. For the sulfur-containing flue gas with medium concentration (the concentration of sulfur dioxide is between 1% and 4%), the acid making process and the disposable desulfurization process are not suitable. Therefore, the flue gas desulfurization process adopting the recoverable sulfur resource is compared with the purification treatment of the medium sulfur-containing flue gas.
At present, the treatment technologies of the sulfur-containing flue gas with medium concentration mainly comprise an ammonia method, a sodium sulfite method, a circulating sodium-alkali method, an ionic liquid method and the like. The flue gas desulfurized by the ammonia method has strong adaptability, no secondary pollution and stable desulfurizer source, but the problem of ammonia escape is not completely solved all the time, and waste slurry is generated after long-term operation, so that the flue gas desulfurized by the ammonia method is not suitable for treating the sulfur-containing flue gas with medium concentration. The circulating sodium-alkali method has the advantages of mature technology, advanced process, low operation cost and high economic benefit, can realize integration of desulfurization and dust removal, but has larger regeneration difficulty of sodium sulfate which is a byproduct of sodium subtraction oxidation in practical application. The ionic liquid absorption method has the advantages of high efficiency, low loss, wide application range and the like, has complete independent intellectual property rights, but has more complex equipment and unobvious advantages when the sulfur content of the flue gas is lower. Chinese patent CN107737520A discloses a method for performing synergistic desulfurization and denitrification on nonferrous smelting flue gas by using a circulating sodium-alkali method, wherein ozone is added into the flue gas to convert NO into NO2Then the coexisting NO in the smoke is treated by sodium sulfite2、SO2Performing synchronous absorption, strengthening the reductive denitrification of nitrite and nitrate in the absorption solution by electrochemical method, regenerating the generated sodium bisulfite by steam heating and nitrogen protection, and simultaneously extracting and concentrating the nitrogen to obtain recyclable high-concentration SO2Finally realizing deep denitration and SO of smelting flue gas2Removal and recycling of the waste water. However, the method of the patent uses the sodium sulfite as a desulfurizing agent, has the advantages of small capacity of absorbing sulfur dioxide, low regeneration efficiency and high operation cost。
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a method for recycling flue gas desulfurization and recovering sulfur dioxide by using an organic magnesium solution.
The purpose of the invention can be realized by the following technical scheme: a method for recycling flue gas desulfurization and sulfur dioxide by using an organic acid magnesium solution is characterized by comprising the following steps:
1) preparing an organic acid solution with a certain concentration and a buffering effect, adding a magnesium oxide solid into the organic acid solution according to a certain stoichiometric ratio, stirring to fully dissolve the magnesium oxide to obtain an organic magnesium solution, and adding a small amount of antioxidant to prepare a desulfurization barren solution;
the organic acid solution is a polybasic acid which is cheap and easy to obtain, easy to dissolve in water, stable in performance and small in corrosivity, can form an easily soluble compound with magnesium, mainly comprises one or more combinations of citric acid, adipic acid, succinic acid and other polybasic organic acids, and has the concentration of 0.2-1 mol/L in terms of the volume of the prepared desulfurization barren solution.
The magnesium oxide is one or more of magnesium oxide, magnesium hydroxide, magnesium carbonate or basic magnesium carbonate, the concentration of magnesium ions in the prepared desulfurization barren solution is 0.2-1.5 mol/L, and the formed organic magnesium can be fully dissolved.
The antioxidant comprises one or more of sodium thiosulfate, p-phenylenediamine, hydroquinone or ascorbic acid, and the addition amount of the antioxidant is that the mass concentration of the antioxidant in the magnesium organic acid solution is 0.1-1%. A small amount of antioxidant is effective to inhibit further oxidation of the absorbed sulfite radicals.
2) Inputting the desulfurization barren solution into a desulfurization tower, and enabling the desulfurization barren solution to be in contact with the flue gas to absorb sulfur dioxide in the flue gas; the organic magnesium solution is fully contacted with the flue gas containing sulfur dioxide in a desulfurizing tower, and the sulfur dioxide is chemically absorbed by utilizing the buffering action of the organic magnesium to gradually form a desulfurizing rich solution; the desulfurizing tower is a spray tower, a packed tower or a plate tower, and is selectedThe gas-liquid ratio of (A) is 3-20L/m3。
3) The absorbed sulfur dioxide is gradually accumulated in the solution in a dissolved state to form a desulfurization rich solution, and when the sulfur dioxide content in the desulfurization rich solution is close to saturation (the sulfur dioxide content in the desulfurization rich solution reaches more than 20 g/L), part of the desulfurization rich solution is sent to a desorption tower for desorption and regeneration;
4) the temperature of the desulfurization rich solution entering the desorption tower is raised to 80-120 ℃ in a steam heating mode, the desulfurization rich solution stays for 0.5-2 hours, sulfur dioxide in the desulfurization rich solution is desorbed and released, and the content of sulfur dioxide in the desorbed desulfurization solution is reduced while high-concentration sulfur dioxide gas is obtained, so that the sulfur dioxide is converted into barren solution; the desorption rate of sulfur dioxide in the regeneration solution is more than 40 percent; the content of sulfur dioxide in the regeneration gas is more than 10 percent, and the regeneration gas can be used as an acid making raw material or a recovered pure sulfur dioxide product;
5) after the lean solution is subjected to heat exchange and is cooled to below 50 ℃, returning to a desulfurizing tower for circulating desulfurization, and repeating the step 2-4;
6) since part of the absorbed sulfur dioxide is oxidized, magnesium sulfate is formed in the solution and gradually accumulates. If the smoke contains NO2And the soluble nitrogen oxides are absorbed by the solution simultaneously to form magnesium nitrate or magnesium nitrite. When the concentration of magnesium sulfate in the solution is accumulated to a certain concentration (when the concentration reaches 5 wt%), taking out part of the regenerated barren solution (20-50% V/V) and conveying the barren solution to an alkalization desalting tank, increasing the pH value by adding a certain amount of magnesium oxide to ensure that the pH value of the solution is above 7.0, converting organic acid and sulfurous acid into insoluble magnesium salt precipitates, still dissolving the magnesium sulfate in the solution, and converting residual bisulfite into insoluble magnesium sulfite precipitates; after separation by settling, the supernatant was mainly a magnesium sulfate solution and was separated from the system. The precipitate is organic magnesium or magnesium sulfite, and can be conveyed back to the desulfurization tower to be re-dissolved at low pH (re-dissolved at pH value lower than 5) for recycling desulfurization. The magnesium oxide added can just compensate the magnesium discharged in the form of magnesium sulfate, and the balance of magnesium in the system can be maintained. Similarly, in the above process, magnesium nitrate and magnesium nitrite can be removed simultaneously.
The flue gas can be absorbed when containing high-valence nitrogen oxides. The magnesium nitrate or nitrite formed by absorption can be discharged out of the system along with magnesium sulfate during the desalting process.
The invention overcomes the problems of the traditional absorption liquid (organic amine or ionic liquid solution desulfurization) in the process of absorbing and desorbing sulfur dioxide, provides that organic acid magnesium salt solution such as magnesium citrate is used for replacing the conventional desulfurizer, organic acid and organic acid salt can form conjugate acid-base pairs in the solution, can slow down the reduction of pH value of the absorption liquid caused by absorbing sulfur dioxide, is beneficial to keeping the absorption liquid at a higher sulfur dioxide absorption level, simultaneously prolongs the effective absorption time of the absorption liquid and increases the absorption capacity. Therefore, the organic magnesium sulfate solution has a good buffering effect on the sulfur dioxide absorption process, the absorption capacity is high, the regeneration temperature is low (80-120 ℃), the regeneration of the conventional sodium sulfite absorption solution needs to be carried out under pressure and heated to over 115 ℃, and simultaneously the obtained sulfate by-products are easily removed, so that the high-efficiency capture, desorption and recovery of the sulfur dioxide are realized. Compared with the prior art, the method has the advantages of lower price of magnesium, less consumption in the reaction with sulfur dioxide and larger economic advantage.
Compared with the prior art, the invention has the following advantages:
1. the organic magnesium sulfate solution has excellent buffering effect on the sulfur dioxide absorption process, large absorption capacity and low regeneration temperature, and sulfate by-products are easy to remove;
2. compared with the organic amine desulfurizer, the cost of the desulfurizer of the method is only about 15 percent, the separation cost of sulfate is only about 20 percent, and the energy consumption of sulfur dioxide desorption can be reduced by about 30 percent;
3. the desulfurizer is more environment-friendly and has no problems of secondary pollution and the like;
4. the method is suitable for sulfur dioxide recovery and resource utilization in industrial flue gas in the fields of energy, metallurgy, chemical industry and the like.
Drawings
FIG. 1 is a flow chart of the method of the present invention.
Detailed Description
The invention is described in detail below with reference to specific figures and examples. The following examples will assist those skilled in the art in further understanding the invention, but are not intended to limit the invention in any way. It should be noted that variations and modifications can be made by persons skilled in the art without departing from the spirit of the invention. All falling within the scope of the present invention.
As shown in fig. 1, a method for recycling flue gas desulfurization and sulfur dioxide recovery by using magnesium organic acid solution comprises the following steps:
1) preparing an organic acid solution with a certain concentration and a buffering effect, adding a magnesium oxide solid into the organic acid solution according to a certain stoichiometric ratio, stirring to fully dissolve the magnesium oxide to obtain an organic magnesium solution, and adding a small amount of antioxidant to prepare a desulfurization barren solution;
the concentration of the organic acid is 0.2-1 mol/L based on the volume of the prepared desulfurization barren solution.
The concentration of magnesium ions in the prepared desulfurization barren solution is 0.2-1.5 mol/L.
The addition amount of the antioxidant is 0.1-1% of the mass concentration of the antioxidant in the organic magnesium acid solution.
2) Inputting the desulfurization barren solution into a desulfurization tower, and enabling the desulfurization barren solution to be in contact with the flue gas to absorb sulfur dioxide in the flue gas; the organic magnesium solution is fully contacted with the flue gas containing sulfur dioxide in a desulfurizing tower, and the sulfur dioxide is chemically absorbed by utilizing the buffering action of the organic magnesium to gradually form a desulfurizing rich solution; the desulfurizing tower is a spray tower, a packed tower or a plate tower, and the selected gas-liquid ratio is 3-20L/m3。
3) The absorbed sulfur dioxide is gradually accumulated in the solution in a dissolved state to form a desulfurization rich solution, and when the sulfur dioxide content in the desulfurization rich solution is close to saturation (the sulfur dioxide content in the desulfurization rich solution reaches more than 20 g/L), part of the desulfurization rich solution is sent to a desorption tower for desorption and regeneration;
4) the temperature of the desulfurization rich solution entering the desorption tower is raised to 80-120 ℃ in a steam heating mode, the desulfurization rich solution stays for 0.5-2 hours, sulfur dioxide in the desulfurization rich solution is desorbed and released, and the content of sulfur dioxide in the desorbed desulfurization solution is reduced while high-concentration sulfur dioxide gas is obtained, so that the sulfur dioxide is converted into barren solution; the desorption rate of sulfur dioxide in the regeneration solution is more than 40 percent; the content of sulfur dioxide in the regeneration gas is more than 10 percent, and the regeneration gas can be used as an acid making raw material or a recovered pure sulfur dioxide product;
5) after the lean solution is subjected to heat exchange and is cooled to below 50 ℃, returning to a desulfurizing tower for circulating desulfurization, and repeating the step 2-4;
6) since part of the absorbed sulfur dioxide is oxidized, magnesium sulfate is formed in the solution and gradually accumulates. If the smoke contains NO2And the soluble nitrogen oxides are absorbed by the solution simultaneously to form magnesium nitrate or magnesium nitrite. When the concentration of magnesium sulfate in the solution is accumulated to a certain concentration (when the concentration reaches 5 wt%), taking out part of the regenerated barren solution (20-50% V/V) and conveying the barren solution to an alkalization desalting tank, increasing the pH value by adding a certain amount of magnesium oxide to ensure that the pH value of the solution is above 7.0, converting organic acid and sulfurous acid into insoluble magnesium salt precipitates, still dissolving the magnesium sulfate in the solution, and converting residual bisulfite into insoluble magnesium sulfite precipitates; after separation by settling, the supernatant was mainly a magnesium sulfate solution and was separated from the system. The precipitate is organic magnesium or magnesium sulfite, and can be conveyed back to the desulfurization tower to be re-dissolved at low pH (re-dissolved at pH value lower than 5) for recycling desulfurization. The magnesium oxide added can just compensate the magnesium discharged in the form of magnesium sulfate, and the balance of magnesium in the system can be maintained. Similarly, in the above process, magnesium nitrate and magnesium nitrite can be removed simultaneously.
Example 1
1. 100mL of 0.3mol/L citric acid solution was prepared, and 1.6g of solid magnesium oxide was added thereto, and the magnesium oxide was completely dissolved by stirring to obtain a magnesium citrate solution.
2. Adding 1mL of ascorbic acid into magnesium citrate, transferring into an absorption bottle, and making it fully contact with flue gas at room temperature, wherein the flow rate of flue gas is 1L/min, and the concentration of sulfur dioxide is 10000 ppm.
3. When the content of sulfur dioxide in the citric acid is close to saturation, the absorption rich solution is transferred into a desorption bottle for heating regeneration, the regeneration temperature is 115 ℃, the retention time is 0.5h, and when the sulfur dioxide is blown out, the concentration of the sulfur dioxide in the absorption solution is reduced and becomes a barren solution.
4. And cooling the absorption barren solution, transferring the absorption barren solution into an absorption bottle for circular desulfurization, wherein the conditions are consistent with the conditions, and desorbing after the absorption solution is saturated.
5. Repeating the absorption and desorption processes to finally complete three rounds of absorption and desorption, wherein the absorption efficiencies of the three rounds are respectively 55%, 61% and 60%, and the desorption efficiencies of the three rounds are respectively 48%, 45% and 42%.
Example 2
1. 100mL of 0.3mol/L citric acid solution was prepared, and 2.0g of solid magnesium oxide was added thereto, and the magnesium oxide was completely dissolved by stirring to obtain a magnesium citrate solution.
2. Adding 1mL of ascorbic acid into magnesium citrate, transferring into an absorption bottle, and making it fully contact with flue gas at room temperature, wherein the flow rate of flue gas is 1L/min, and the concentration of sulfur dioxide is 10000 ppm.
3. When the content of sulfur dioxide in the citric acid is close to saturation, the absorption rich solution is transferred into a desorption bottle for heating regeneration, the regeneration temperature is 115 ℃, the retention time is 0.5h, and when the sulfur dioxide is blown out, the concentration of the sulfur dioxide in the absorption solution is reduced and becomes a barren solution.
4. And cooling the absorption barren solution, transferring the absorption barren solution into an absorption bottle for circular desulfurization, wherein the conditions are consistent with the conditions, and desorbing after the absorption solution is saturated.
5. Repeating the absorption and desorption processes to finally complete three rounds of absorption and desorption, wherein the absorption efficiencies of the three rounds are respectively 60%, 64% and 63%, and the desorption efficiencies of the three rounds are respectively 47%, 45% and 44%.
Example 3
1. 100mL of 0.4mol/L citric acid solution was prepared, and 2.0g of solid magnesium oxide was added thereto, and the magnesium oxide was completely dissolved by stirring to obtain a magnesium citrate solution.
2. Adding 1mL of ascorbic acid into magnesium citrate, transferring into an absorption bottle, and making it fully contact with flue gas at room temperature, wherein the flow rate of flue gas is 1L/min, and the concentration of sulfur dioxide is 10000 ppm.
3. When the content of sulfur dioxide in the citric acid is close to saturation, the absorption rich solution is transferred into a desorption bottle for heating regeneration, the regeneration temperature is 115 ℃, the retention time is 0.5h, and when the sulfur dioxide is blown out, the concentration of the sulfur dioxide in the absorption solution is reduced and becomes a barren solution.
4. And cooling the absorption barren solution, transferring the absorption barren solution into an absorption bottle for circular desulfurization, wherein the conditions are consistent with the conditions, and desorbing after the absorption solution is saturated.
5. Repeating the absorption and desorption processes to finally complete three rounds of absorption and desorption, wherein the three rounds of absorption efficiencies are respectively 61%, 66% and 65%, and the three rounds of desorption efficiencies are respectively 45%, 43% and 42%.
Claims (9)
1. A method for recycling flue gas desulfurization and sulfur dioxide by using an organic acid magnesium solution is characterized by comprising the following steps:
1) adding magnesium oxide solid into the organic acid solution according to the stoichiometric ratio, stirring to fully dissolve the magnesium oxide to obtain an organic magnesium solution, and adding an antioxidant to prepare a desulfurization barren solution;
2) inputting the desulfurization barren solution into a desulfurization tower, and enabling the desulfurization barren solution to be in contact with the flue gas to absorb sulfur dioxide in the flue gas;
3) the absorbed sulfur dioxide is gradually accumulated in the solution in a dissolved state to form a sulfur-removing rich solution, and when the content of the sulfur dioxide in the sulfur-removing rich solution is close to saturation, part of the sulfur-removing rich solution is sent to a desorption tower for desorption and regeneration;
4) the temperature of the desulfurization rich solution entering the desorption tower is raised, so that the sulfur dioxide in the desulfurization rich solution is desorbed and released, and the sulfur dioxide content in the desorbed desulfurization solution is reduced and converted into barren solution while high-concentration sulfur dioxide gas is obtained;
5) after heat exchange and temperature reduction, the barren solution returns to the desulfurizing tower for circulating desulfurization, and the step 2-4 is repeated;
6) when the concentration of magnesium sulfate in the barren solution reaches 5%, sending 20% -50% of the solution to an alkalization desalting tank, adjusting the alkalinity of the solution by using magnesium oxide to ensure that the pH value of the solution is above 7.0, and enabling organic acid in the solution to form insoluble magnesium salt precipitate and converting residual bisulfite into insoluble magnesium sulfite precipitate; and performing solid-liquid separation on the obtained suspension, returning the recovered precipitate to a desulfurizing tower, re-dissolving when the pH value is lower than 5, and continuously performing the desulfurization, wherein the supernatant is mainly magnesium sulfate solution and is discharged from the circulating solution.
2. The method according to claim 1, wherein the organic acid solution in step 1) is a polybasic organic acid solvent comprising one or more of citric acid, adipic acid and succinic acid, and the organic acid has a concentration of 0.2-1 mol/L based on the volume of the prepared desulfurization barren solution.
3. The method for recycling flue gas desulfurization and sulfur dioxide according to claim 1, wherein the concentration of magnesium ions in the desulfurization barren solution prepared in step 1) is 0.2-1.5 mol/L.
4. The method according to claim 1, wherein the antioxidant in step 1) comprises one or more of sodium thiosulfate, p-phenylenediamine, hydroquinone and ascorbic acid, and the antioxidant is added in an amount of 0.1-1% by mass in the magnesium organic acid solution.
5. The method for recycling flue gas desulfurization and sulfur dioxide recovery using magnesium organate solution as claimed in claim 1, wherein said desulfurization tower is a spray tower, a packed tower or a tray tower, and the selected gas-liquid ratio is 3-20L/m3When the sulfur dioxide content in the desulfurization rich solution reaches more than 20g/L, the desulfurization rich solution is sent to a desorption tower for desorption and regeneration.
6. The method for recycling flue gas desulfurization and sulfur dioxide by using the magnesium organic acid solution according to claim 1, wherein the regeneration temperature of the desulfurization rich solution in the step 4) in the desorption tower is 80-120 ℃, the regeneration retention time is 0.5-2 hours, and the desorption rate of sulfur dioxide in the solution is more than 40%; the content of sulfur dioxide in the regeneration gas is more than 10 percent, and the regeneration gas can be used as an acid making raw material or a recovered pure sulfur dioxide product.
7. The method for recycling flue gas desulfurization and sulfur dioxide recovery by using magnesium organate solution as claimed in claim 1, wherein the barren solution of step 5) is cooled to below 50 ℃ and returned to the desulfurization tower for recycling absorption of sulfur dioxide.
8. The method for recycling flue gas desulfurization and sulfur dioxide according to claim 1, wherein the magnesium oxide and the water added into the alkalization desalting tank of step 6) are just enough to supplement the loss of the desalted liquid discharge, and the balance between the magnesium oxide and the water is achieved.
9. The method for recycling flue gas desulfurization and sulfur dioxide according to claim 1, wherein the flue gas containing nitrogen oxides with high valence state can be absorbed simultaneously, and the absorbed magnesium nitrate or magnesium nitrite is discharged out of the system along with magnesium sulfate during the process of desalting.
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| CN1891330A (en) * | 2005-07-05 | 2007-01-10 | 熊天渝 | Method for removing sulfur dioxide from wastegas for making it be a product by circulation of magnesium oxide |
| 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 |
| CN101607173A (en) * | 2008-06-17 | 2009-12-23 | 陆泳凯 | The sulfur removal technology of using external regenerative cycle magnesium sulfate method flue gas or waste gas |
| CN102886199A (en) * | 2012-10-26 | 2013-01-23 | 煤炭工业济南设计研究院有限公司 | Flue gas desulfurization device and desulfurization method by magnesium oxide process |
| CN110844926A (en) * | 2019-12-17 | 2020-02-28 | 江苏联慧资源环境科技有限公司 | Production method of high-purity magnesium sulfite |
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