CN219023798U - Flue gas desulfurization device - Google Patents
Flue gas desulfurization device Download PDFInfo
- Publication number
- CN219023798U CN219023798U CN202223060854.8U CN202223060854U CN219023798U CN 219023798 U CN219023798 U CN 219023798U CN 202223060854 U CN202223060854 U CN 202223060854U CN 219023798 U CN219023798 U CN 219023798U
- Authority
- CN
- China
- Prior art keywords
- desulfurizing agent
- outlet
- flue gas
- tower
- unit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a flue gas desulfurization device, which comprises an absorption tower, a desulfurizing agent storage tank and a filtering unit, wherein flue gas to be treated is communicated with an air inlet of the absorption tower, and an air outlet of the absorption tower is communicated with air; the first outlet of the filtering unit is connected with the inlet of the cathode chamber of the proton circulation electrolytic cell,the outlet of the cathode chamber is connected with a desulfurizing agent storage tank, desulfurizing agent lean solution which is conveyed to the cathode chamber of the proton circulation electrolytic tank is regenerated into desulfurizing agent through electrochemical reaction, and the desulfurizing agent lean solution is returned to the desulfurizing agent storage tank for recycling; the second outlet of the filtering unit is connected with the first liquid inlet of the desorption tower, the second liquid inlet of the desorption tower is connected with the outlet of the anode chamber of the proton circulation electrolytic tank, the desulfurizing agent lean liquid conveyed to the desorption tower is mixed with the anode liquid of the proton circulation electrolytic tank, and SO is released under the action of negative pressure 2 SO is arranged on the desorption tower 2 And an air outlet. The method can realize the cyclic regeneration of the desulfurizing agent and remove sulfur dioxide in the flue gas with low cost and low energy consumption.
Description
Technical Field
The utility model relates to a desulfurization technology, in particular to a flue gas desulfurization device.
Background
In coal-fired power plants and natural gas purification, sulfur dioxide in tail gas needs to be removed, and the tail gas is ensured to reach the emission standard. Taking a coal-fired power plant as an example, the average sulfur content of coal is about 1%, more than 40 hundred million tons of coal are consumed each year, and SO is produced each year 2 Up to about 6400 ten thousand tons, the total amount of desulfurization is enormous. While the produced natural gas contains H 2 S, H is obtained by dry oxidation 2 S is oxidized to form sulfur and water, and SO is generated due to excessive oxidation 2 The tail gas is discharged after desulfurization treatment. In the state of economic high-speed development in China, controlling the total emission amount of sulfur dioxide is always a key source for controlling air pollution, and the SO content is over 90 percent at present 2 Emissions originate from coal burning, 50% of which are consumed from coal burning plants, thus controlling SO produced by tail gas from coal burning plants 2 Is the important thing. Meanwhile, china is a very sulfur-poor country, and more than 1000 ten thousand tons of sulfur are imported annually for preparing SO 2 Producing sulfuric acid, sodium metabisulfite, sodium sulfite and other downstream vulcanized products. Therefore, whether the recycling of sulfur dioxide in the flue gas can be realized is the biggest challenge of solving the shortage of sulfur resources and environmental pollution in China.
The most widely used desulfurization method of coal-fired power plants at present is a limestone-gypsum desulfurization process, namely: grinding limestone (calcium carbonate) into fine powder, pulping with water, spraying into fine droplets, and countercurrent contacting with flue gas in desulfurizing tower to obtain SO in flue gas 2 The reaction of oxygen in air with limestone produces gypsum (calcium sulfate) and the chemical reaction takes place as follows:
CaCO 3 +SO 2 +1/2H 2 O→CaSO 3 ·1/2H 2 O+CO 2 ，
Ca(OH) 2 +SO 2 →CaSO 3 ·1/2H 2 O+1/2H 2 O，
CaSO 3 ·1/2H 2 O+SO 2 +1/2H 2 O→Ca(HSO 3 ) 2 ，
2CaSO 3 ·1/2H 2 O+O 2 +3H 2 O→2CaSO 4 ·2H 2 O，
Ca(HSO 3 ) 2 +O 2 +2H 2 O→CaSO 4 ·2H 2 O+H 2 SO 4 。
from the reaction equation, SO in the flue gas 2 Fixed in the form of gypsum solid and simultaneously discharges CO 2 The process is also a technical route with best economy and the widest adaptability in the large-scale industrialized desulfurization process at present, but the process also has certain limitations:
1. the core chemical reaction of the desulfurization method is a gas-liquid-solid three-phase reaction, the phase interface is more, the mass transfer resistance is large, and the desulfurized flue gas can only reach 200mg/Nm or less of SO2 of a newly built coal-fired boiler in a key region in GB13271-2014 emission Standard of atmospheric pollutants of boiler in general 3 Cannot reach 35mg/Nm 3 The ultra-clean emission index of (2) can reach the standard only by increasing the sodium hydroxide absorption mode, the operation cost is high, and the salt-containing wastewater is generated;
2. limestone is a natural mineral resource, and large-scale use of limestone as a desulfurizing agent can lead to large-scale mining, and has great negative influence on ecological environment;
3. the dihydrate gypsum slurry produced by desulfurization can be sold as a gypsum product after being subjected to filter pressing and drying, so that the energy consumption and the water consumption are high;
4. the byproduct dihydrate gypsum inevitably contains limestone and impurities brought by flue gas, has low quality, can only aim at a low-end market, has the total yield of the desulfurization gypsum of over 1.3 hundred million tons per year, is difficult to be completely consumed by the market, and has the difficult problem of waste solid piling;
5. in the process of providing a calcium source by the participation of calcium carbonate in the reaction, equimolar amount of carbon dioxide is released, and the carbon reduction trend of the 'two carbon' policy is not met.
Therefore, how to remove sulfur dioxide in flue gas and tail gas with low cost and low energy consumption to produce sulfur products with high added value, and realize the recycling of sulfur in flue gas and tail gas, is one of the core problems to be solved by the novel desulfurization technology, and needs to develop a novel desulfurization technology.
Disclosure of Invention
The utility model aims to provide a flue gas desulfurization device which can realize the cyclic regeneration of a desulfurizing agent, remove sulfur dioxide in flue gas and tail gas with low cost and low energy consumption, so that sulfur products with high added value are produced, and the recycling of sulfur in the flue gas and tail gas is realized.
The flue gas desulfurization device comprises an absorption tower, a desulfurizing agent storage tank communicated with a liquid inlet of the absorption tower and a filtering unit communicated with a liquid outlet of the absorption tower, wherein flue gas to be treated is communicated with an air inlet of the absorption tower, and an air outlet of the absorption tower is communicated with air; the first outlet of the filtering unit is connected with the inlet of the cathode chamber of the proton circulation electrolytic cell, the outlet of the cathode chamber is connected with the desulfurizing agent storage tank, the desulfurizing agent lean solution conveyed to the cathode chamber of the proton circulation electrolytic cell is regenerated into desulfurizing agent through electrochemical reaction, and the desulfurizing agent lean solution is returned to the desulfurizing agent storage tank for recycling; the second outlet of the filtering unit is connected with the first liquid inlet of the desorption tower, the second liquid inlet of the desorption tower is connected with the outlet of the anode chamber of the proton circulation electrolytic cell, the desulfurizing agent lean liquid conveyed to the desorption tower is mixed with the anode liquid of the proton circulation electrolytic cell, and SO is released under the action of negative pressure 2 SO is arranged on the desorption tower 2 And an air outlet.
Further, the device also comprises a denitration unit connected with the liquid outlet of the desorption tower, wherein the denitration unit is used for removing sulfate radical in the desorbed desulfurizing agent lean solution; the first liquid outlet of the denitration unit is connected with the evaporation unit, and the second liquid outlet of the denitration unit is connected with the mirabilite crystallization unit; the evaporation unit is used for evaporating redundant water in the denitrified desulfurizing agent lean solution, and a liquid outlet of the evaporation unit is connected with an anode chamber inlet of the proton circulation electrolytic tank; the mirabilite crystallization unit is used for carrying out freezing crystallization treatment on the nitrate-rich solution of the denitration unit.
Further, the denitration unit is a nanofiltration membrane.
Further, the desorption tower is SO 2 The air outlet is connected with a vacuum pump through vacuumThe pump provides negative pressure to the desorber.
Further, the desorption tower is SO 2 A cooler is connected between the air outlet and the vacuum pump.
Further, the filtering unit comprises an ultrafiltration filter and a resin tower which are connected in sequence, wherein the ultrafiltration filter is used for removing dust particles in the desulfurizing agent lean solution, and the resin tower is used for removing calcium and magnesium ions in the desulfurizing agent lean solution.
Compared with the prior art, the utility model has the following beneficial effects.
1. The utility model absorbs and captures SO in the flue gas through the desulfurizing agent in the absorption tower 2 The desulfurizing agent absorbs SO 2 Becomes a desulfurizing agent lean solution, and after the desulfurizing agent lean solution is filtered by a filtering unit, part of the desulfurizing agent lean solution is pumped to a cathode chamber of a proton circulation electrolytic tank, and the other part of the desulfurizing agent lean solution is pumped to a desorption tower; the desulfurizing agent lean solution pumped to the cathode chamber of the proton circulation electrolytic tank is regenerated into desulfurizing agent through electrochemical reaction, and the desulfurizing agent lean solution returns to a desulfurizing agent storage tank for recycling; mixing the desulfurizing agent lean solution pumped to the desorption tower with anode solution from a proton circulation electrolytic tank, and releasing SO under the action of negative pressure 2 The generated sulfur dioxide gas is sent downstream as a raw material to produce a related sulfur product. SO desorbed by the device 2 Only contains saturated water, can be further processed into sulfur products according to the requirements of downstream devices, omits the traditional sulfur chemical industry to calcine sulfur or pyrite and purify to obtain SO 2 At very low cost, high quality SO necessary for the vulcanizer industry 2 Raw materials.
2. The device also comprises a denitration unit, the desorbed desulfurizing agent lean solution is sent to the denitration unit, sulfate radicals generated by air oxidation are removed, and the denitrified desulfurizing agent lean solution is pumped into an evaporation unit; evaporating excessive water from the desulfurizing agent lean solution, and returning the water to the cathode; the evaporated solution is sent into an anode chamber of a proton circulation electrolytic tank, and anode liquid is generated through electrochemical reaction and circulated back to a desorption tower for use. The nitrate-rich solution of the denitration unit is further frozen and crystallized to obtain a byproduct sodium sulfate decahydrate, and the byproduct sodium sulfate decahydrate is sold as a byproduct after centrifugal separation, so that the recycling utilization is realized.
Drawings
FIG. 1 is a schematic diagram of a flue gas desulfurization apparatus according to the present utility model.
In the figure, a 1-absorption tower, a 2-desorption tower, a 3-proton circulation electrolytic tank, a 31-cathode chamber, a 32-anode chamber, a 33-anolyte storage tank, a 4-cooler, a 5-vacuum pump, a 6-denitration unit, a 7-evaporation unit, an 8-mirabilite crystallization unit, a 9-centrifugal unit, a 10-ultrafiltration filter, an 11-resin tower, a 12-crude desulfurizing agent lean solution tank, a 13-fine desulfurizing agent lean solution tank, a 14-ultrapure desulfurizing agent lean solution tank, a 15-desulfurizing agent storage tank, 16-flue gas to be treated, 17-exhaust gas, 18-sulfur dioxide gas and 19-byproducts.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present utility model more apparent, the technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are only some embodiments of the present utility model, not all embodiments of the present utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1, the flue gas desulfurization apparatus shown comprises an absorption tower 1, a desulfurizing agent storage tank 15 communicated with a liquid inlet of the absorption tower 1, and a filtering unit communicated with a liquid outlet of the absorption tower 1, wherein flue gas 16 to be treated is communicated with an air inlet of the absorption tower 1, and an air outlet of the absorption tower 1 is communicated with air. The desulfurizing agent in the desulfurizing agent storage tank 15 is pumped into the absorption tower 1 to be contacted and reacted with the flue gas 16 to be treated, namely the flue gas of the coal-fired boiler at 80-350 ℃, and SO in the flue gas 2 After absorption and reaction by the desulphurisation agent, the SO in the exhaust gas 17 2 Concentration of less than 5mg/Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the The desulfurizing agent absorbs SO 2 Becomes a desulfurizing agent lean solution.
In this embodiment, the desulfurizing agent is an existing sulfite-based desulfurizing agent, and is used for SO at pH 8-10 2 Has extremely high absorption efficiency, and the flue gas is removed by the absorption tower 1SO in the exhaust gas after sulfur reaction 2 ≤5mg/Nm 3 The desulfurization efficiency is obviously higher than that of the limestone-gypsum method, and the absorption effect of sodium hydroxide solution is comparable.
The first outlet of the filtering unit is connected with the inlet of the cathode chamber 31 of the proton circulation electrolytic tank 3, the outlet of the cathode chamber 31 is connected with the desulfurizing agent storage tank 1, the desulfurizing agent lean solution conveyed to the cathode chamber 31 of the proton circulation electrolytic tank 3 is regenerated into desulfurizing agent through electrochemical reaction, and the desulfurizing agent is returned to the desulfurizing agent storage tank 15 for recycling. The second outlet of the filtering unit is connected with the first liquid inlet of the desorption tower 2, the second liquid inlet of the desorption tower 2 is connected with the outlet of the anode chamber 32 of the proton circulation electrolytic tank 3, and the desorption tower 2 is provided with SO 2 And an air outlet. SO of the desorption column 2 2 The gas outlet is connected with a vacuum pump 5, and the SO of the desorption tower 2 2 A cooler 4 is connected between the air outlet and a vacuum pump 5, and negative pressure is provided for the desorption tower 2 through the vacuum pump. The desulfurizing agent lean solution delivered to the desorption tower 2 is mixed with the anode solution of the proton circulation electrolytic tank 3, and SO is released under the action of negative pressure 2 I.e. under the action of negative pressure to realize SO 2 And the high-purity sulfur dioxide gas 18 is obtained after the saturated water content is reduced by the treatment of the cooler 4, and the high-purity sulfur dioxide gas 18 is sent to downstream liquefaction for sale or is continuously processed into chemical products with higher added values such as sulfuric acid, sodium metabisulfite and the like, thereby realizing the recycling of sulfur in the flue gas. SO desorbed by the device 2 Only contains saturated water, can be further processed into sulfur products according to the requirements of downstream devices, omits the traditional sulfur chemical industry to calcine sulfur or pyrite and purify to obtain SO 2 At very low cost, high quality SO necessary for the vulcanizer industry 2 Raw materials.
The proton circulation electrolytic cell 3 is capable of ionizing water under the condition that the cell voltage is less than 1V to obtain hydrogen ions and hydroxyl ions at the anode and the cathode, respectively. After the desulfurizing agent lean solution treated by the filtering unit enters the cathode of the proton circulation electrolytic tank 3, the desulfurizing agent lean solution is combined with hydroxide radicals generated by the proton circulation electrolytic tank, and sodium ions which migrate from the anode side of the proton circulation ionic membrane to the cathode are combined under the action of current, so that the sodium sulfite desulfurizing agent is regenerated. At the same time, sodium salt from the evaporation unit 7 is sent to the anode side of the proton circulation electrolytic tank 3, converted into monovalent weak acid and sent to a desorption tower to help realize that sulfite ions are desorbed out of SO under acidic condition 2 And (3) gas.
The liquid outlet connection of the desorption tower 2 is connected with a denitration unit 6, and the denitration unit 6 is a nanofiltration membrane. Sulfate radical generated by air oxidation is removed through the selective interception of divalent ions by the nanofiltration membrane. The first liquid outlet of denitration unit 6 is connected with evaporation unit 7, and the second liquid outlet of denitration unit 6 is connected with mirabilite crystallization unit 8. The evaporation unit 7 is used for evaporating excessive water in the denitrified desulfurizing agent lean solution, the evaporated water is returned to the cathode chamber 31 of the proton circulation electrolytic tank 3, the liquid outlet of the evaporation unit 7 is connected with the anolyte storage tank 33, the anolyte storage tank 33 is connected with the inlet of the anode chamber 32 of the proton circulation electrolytic tank 3, the evaporated solution is sent into the anode chamber of the proton circulation electrolytic tank 3, and the anolyte is generated through electrochemical reaction and is circulated back to the desorption tower 2 for use. The nitrate-rich solution of the denitration unit 6 is subjected to freezing crystallization by the mirabilite crystallization unit 8 to obtain byproduct sodium sulfate decahydrate, and then is treated by the centrifugal unit 9 to be sold as a byproduct. The desorbed desulfurizing agent lean solution utilizes the interception characteristic of the denitration unit to divalent ions, realizes the separation of sulfate radicals, and enables the sulfate radicals to leave the circulating system in a byproduct sodium sulfate decahydrate mode.
The filtering unit comprises an ultrafiltration filter 10 and a resin tower 11 which are connected in sequence, wherein the ultrafiltration filter 10 is used for removing dust particles in the desulfurizing agent lean solution, and the resin tower 11 is used for removing calcium and magnesium ions in the desulfurizing agent lean solution. A crude desulfurizing agent lean solution tank is connected between the absorption tower 1 and the ultrafiltration filter 10, a fine desulfurizing agent lean solution tank 13 is connected between the ultrafiltration filter 10 and the resin tower 11, a liquid outlet of the resin tower 11 is an ultrapure desulfurizing agent lean solution tank 14, and a liquid outlet of the ultrapure desulfurizing agent lean solution tank 14 is connected with the desorption tower 2 and the proton circulation electrolytic tank 3. The desulfurizing agent lean solution discharged from the absorption tower 1 is subjected to ultrafiltration and ion exchange resin adsorption to remove particulate matters and calcium and magnesium ions, so that the desulfurizing agent lean solution meets the requirement of returning to the proton circulation electrolytic tank 3.
The foregoing description of the preferred embodiments of the present application is not intended to be limiting, but is intended to cover any and all modifications, equivalents, and alternatives falling within the spirit and principles of the present application.
Claims (6)
1. A flue gas desulfurization device, characterized in that: the flue gas treatment device comprises an absorption tower (1), a desulfurizing agent storage tank (15) communicated with a liquid inlet of the absorption tower (1) and a filtering unit communicated with a liquid outlet of the absorption tower (1), wherein flue gas (16) to be treated is communicated with an air inlet of the absorption tower (1), and an air outlet of the absorption tower (1) is communicated with air;
the first outlet of the filtering unit is connected with the inlet of a cathode chamber (31) of the proton circulation electrolytic cell (3), the outlet of the cathode chamber (31) is connected with a desulfurizing agent storage tank (15), desulfurizing agent lean solution which is conveyed to the cathode chamber (31) of the proton circulation electrolytic cell (3) is regenerated into desulfurizing agent through electrochemical reaction, and the desulfurizing agent is returned to the desulfurizing agent storage tank (15) for recycling;
the second outlet of the filtering unit is connected with the first liquid inlet of the desorption tower (2), the second liquid inlet of the desorption tower (2) is connected with the outlet of the anode chamber (32) of the proton circulation electrolytic tank (3), the desulfurizing agent lean liquid conveyed to the desorption tower (2) is mixed with the anode liquid of the proton circulation electrolytic tank (3), and SO is released under the action of negative pressure 2 SO is arranged on the desorption tower (2) 2 And an air outlet.
2. The flue gas desulfurization device according to claim 1, wherein: the device also comprises a denitration unit (6) connected with the liquid outlet of the desorption tower (2), wherein the denitration unit (6) is used for removing sulfate radical in the desorbed desulfurizing agent lean solution;
the first liquid outlet of the denitration unit (6) is connected with the evaporation unit (7), and the second liquid outlet of the denitration unit (6) is connected with the mirabilite crystallization unit (8);
the evaporation unit (7) is used for evaporating redundant water in the denitrified desulfurizing agent lean solution, and a liquid outlet of the evaporation unit (7) is connected with an inlet of an anode chamber (32) of the proton circulation electrolytic tank (3);
the mirabilite crystallization unit (8) is used for carrying out freezing crystallization treatment on the rich-nitrate solution of the denitration unit (6).
3. The flue gas desulfurization device according to claim 2, wherein: the denitration unit (6) is a nanofiltration membrane.
4. The flue gas desulfurization device according to claim 1 or 2, characterized in that: SO of the desorption tower (2) 2 The air outlet is connected with a vacuum pump (5), and negative pressure is provided for the desorption tower (2) through the vacuum pump (5).
5. A flue gas desulfurization device according to claim 3, wherein: SO of the desorption tower (2) 2 A cooler (4) is connected between the air outlet and the vacuum pump (5).
6. The flue gas desulfurization device according to claim 1 or 2, characterized in that: the filtering unit comprises an ultrafiltration filter (10) and a resin tower (11) which are sequentially connected, wherein the ultrafiltration filter (10) is used for removing dust particles in the desulfurizing agent lean solution, and the resin tower (11) is used for removing calcium and magnesium ions in the desulfurizing agent lean solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223060854.8U CN219023798U (en) | 2022-11-17 | 2022-11-17 | Flue gas desulfurization device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223060854.8U CN219023798U (en) | 2022-11-17 | 2022-11-17 | Flue gas desulfurization device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219023798U true CN219023798U (en) | 2023-05-16 |
Family
ID=86289713
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223060854.8U Active CN219023798U (en) | 2022-11-17 | 2022-11-17 | Flue gas desulfurization device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219023798U (en) |
-
2022
- 2022-11-17 CN CN202223060854.8U patent/CN219023798U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102151476B (en) | Method for removing hydrogen sulfide in gas phase through oxidization under high gravity field | |
| CN111924807A (en) | Method and device for trapping carbon dioxide and simultaneously producing sulfuric acid by sodium bisulfate | |
| CN103303877B (en) | Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process | |
| CN103203174B (en) | SO in a kind of trapping coal-fired plant flue gas 2and CO 2and the method for production chemical product | |
| CN102489132B (en) | Novel dual-alkali desulfurization method for removal of sulfur dioxide from flue gas and generation of elemental sulfur as byproduct | |
| CN103230734B (en) | Combine the method removing sulfur dioxide in flue gas and nitrogen oxide | |
| CA2952395A1 (en) | Process and device for desulfurization-denitration of flue gas | |
| CN101422693A (en) | Sulphuric acid tail-gas deep desulfurization method | |
| CN109095732B (en) | Process for preparing high-purity magnesium hydroxide based on magnesium-method desulfurization wastewater | |
| CN112915755B (en) | System and method for jointly recovering sulfur dioxide in flue gas and removing nitrogen oxide | |
| CN112499651A (en) | Method and device for preparing sodium bicarbonate by electrochemically capturing carbon dioxide | |
| CN110683544A (en) | Method for improving concentration of carbon dioxide in tail gas of lime rotary kiln | |
| CN102225307A (en) | Flue gas desulfurization process by using organic acid enhanced acetylene sludge | |
| CN113856441A (en) | Ammonia desulfurization method and ammonia desulfurization apparatus | |
| CN106318500A (en) | Biological purifying process of unconventional gas | |
| CN108261913B (en) | Magnesium oxide semi-dry desulfurization process | |
| CN110124451A (en) | SO in wet type substep removing flue gas2With the method for NO | |
| CN219023798U (en) | Flue gas desulfurization device | |
| CN1339332A (en) | Sulphur dioxide removing electrolysis process | |
| CN109260928B (en) | Ammonium bicarbonate desulfurization method and device with synergy of lead plaster desulfurization and flue gas desulfurization | |
| CN111729474A (en) | Method for circulating flue gas desulfurization and sulfur dioxide recovery by using organic acid magnesium solution | |
| CN102485325B (en) | Flue gas desulphurization technology with ammonium sulfate-calcium hydroxide slurry method | |
| CN212236673U (en) | Material balance processing system in limestone wet desulphurization absorption tower slurry | |
| CN106994292A (en) | A kind of desulfurizing agent and its application, and using the desulphurization system of the desulfurizing agent | |
| CN111437701A (en) | System and method for balancing and treating materials in slurry of limestone wet desulphurization absorption tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |