CN1428186A - Sodium base or magnesium base wet flue gas desulfurizing system capable of completely recovering by-product without wastes - Google Patents
Sodium base or magnesium base wet flue gas desulfurizing system capable of completely recovering by-product without wastes Download PDFInfo
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- CN1428186A CN1428186A CN 01144928 CN01144928A CN1428186A CN 1428186 A CN1428186 A CN 1428186A CN 01144928 CN01144928 CN 01144928 CN 01144928 A CN01144928 A CN 01144928A CN 1428186 A CN1428186 A CN 1428186A
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- pipe
- flue gas
- desulfurization
- nozzle
- product
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 239000003546 flue gas Substances 0.000 title claims abstract description 42
- 239000006227 byproduct Substances 0.000 title claims abstract description 25
- 239000011734 sodium Substances 0.000 title claims abstract description 17
- 239000011777 magnesium Substances 0.000 title claims abstract description 16
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 title claims abstract description 15
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 15
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 15
- 229910052708 sodium Inorganic materials 0.000 title claims abstract description 15
- 239000002699 waste material Substances 0.000 title claims abstract description 10
- 230000003009 desulfurizing effect Effects 0.000 title description 5
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 36
- 230000023556 desulfurization Effects 0.000 claims abstract description 36
- 238000010521 absorption reaction Methods 0.000 claims abstract description 28
- 239000000243 solution Substances 0.000 claims abstract description 20
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 13
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 9
- 239000012670 alkaline solution Substances 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 230000003647 oxidation Effects 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000000047 product Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000011001 backwashing Methods 0.000 claims description 3
- 238000007791 dehumidification Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 2
- 239000007795 chemical reaction product Substances 0.000 claims 1
- 230000018044 dehydration Effects 0.000 claims 1
- 238000006297 dehydration reaction Methods 0.000 claims 1
- 239000000945 filler Substances 0.000 claims 1
- 238000011084 recovery Methods 0.000 claims 1
- 239000012266 salt solution Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 claims 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract 2
- 239000003517 fume Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000779 smoke Substances 0.000 description 4
- UIIMBOGNXHQVGW-UHFFFAOYSA-M sodium bicarbonate Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical group [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000007832 Na2SO4 Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The present invention discloses a sodium base or magnesium base wet flue gas desulfurization system for completely recovering by-product without wastes, and is characterized by that said absorption tower is made into the form of cylinder, its top is connected with fume exhaust pipe, and its interior is equipped with dehumidifying grating, back rinsing pipe with nozzle, upper band nozzle pipe, separation cover and lower band nozzle pipe. The sodium base or magnesium base alkaline solution can be flowed into the upper and lower band nozzle places from exterior through supply pipe, passes through the nozzle and downward sprayed, and the hot flue gas is flowed upward from lower portion, and can be backward mixed with alkaline solution, and reacted in absorption zone and oxidation zone, the sulfur dioxide in the flue gas can be absorbed, and oxide into sulfate solution which can be discharged from lower portion, concentrated, dehydrated and fed into evaporator.
Description
The technical field is as follows:
the invention relates to a wet flue gas desulfurization system, in particular to a sodium-based or magnesium-based wet flue gas desulfurization system capable of completely recovering byproducts without wastes.
Secondly, background art:
the wet flue gas desulfurization system has high desulfurization efficiency, good adaptability to flue gas and desulfurizer, and can be used for large-capacity flue gas purification, so that it has the most extensive application, such as calcium base (calcium oxide CaO or calcium carbonate CaCO)3) Desulfurization systems, etc., but have the disadvantage of being prone to fouling, wear, and plugging of the piping, thereby reducing operational reliability. Meanwhile, the byproduct is calcium sulfate slag slurry which is difficult to dissolve in water, and the waste liquid and the waste slag are difficult to treat, so that secondary pollution is generated. Using sodium (hydrogen) with good performanceNaOH or Na sodium carbonate2CO3Sodium bicarbonate NaHCO3) Or magnesium based (magnesium hydroxide Mg (OH)2) The desulfurizing agent has the disadvantage of high price. Therefore, the aim of realizing high-efficiency and economic flue gas desulfurization by completely recycling the byproducts of sodium-based and magnesium-based desulfurization and improving the economic benefit is sought.
Thirdly, the invention content:
the invention aims to provide a desulfurization system which has high desulfurization efficiency, compact and simple structure, low cost and complete recycling of byproducts.
The system mainly comprises an evaporator, a filter bag type collector, cylindrical desulfurization absorption tower equipment, a relevant connecting pipeline, a water pump, a fan and the like. The absorption tower is internally provided with a dehumidification grid, a backwashing pipe with a nozzle, an upper nozzle pipe, a separation cover and a lower nozzle pipe from top to bottom in sequence along the height, an alkaline solution supply pipe is arranged at one side and connected to the nozzle pipe, so that alkaline solution is sprayed downwards, hot flue gas is introduced into one side of the lower part and flows from bottom to top, the two parts are uniformly mixed in reverse directions to carry out desulfurization and oxidation reactions, sulfate solution is formed to flow to the lower part, a lower circulating pump extracts the sulfate solution, the sulfate solution is conveyed to a thickener through a recycling pipe to be dehydrated and then enters the nozzle pipe with the evaporator, the hot flue gas fed from the upper part of the evaporator is evaporated to dryness and then is conveyed to a collector to carry out solid particle and flue gas separation, the product is a byproduct, the flue gas enters the absorption tower, and is discharged from the top after acid gas is removed.
The advantages of such a system are:
1. sodium base or magnesium base with excellent performance is used as a desulfurizing agent, and the desulfurizing efficiency can reach more than 98 percent.
2. Simple and compact structure, no scaling and no blockage in the desulfurization reaction system, reliable operation and convenient operation.
3. The desulfurization absorption reaction and the oxidation reaction of the by-product are respectively and independently operated in the absorption tower, and the operation is easy
In the control, the by-product components reach the optimum state. The separation and collection rate of the product is as high as more than 99%.
4. Flue gasis used as a drying agent, the by-products are completely dried and recovered, no waste liquid or waste residue is discharged, and the drying is carried out
The exhausted gas returns to the absorption tower again for desulfurization and absorption reaction, so that the acid gas in the flue gas is effectively removed
And (3) a body.
Fourthly, explanation of the attached drawings:
the figure is a schematic structural diagram of a sodium-based or magnesium-based wet flue gas desulfurization system for completely recovering byproducts and having no waste.
As shown in the figure, a barrel-shaped desulfurization absorption tower (12) is barrel-shaped, flue gas to be purified enters from one side of the barrel-shaped desulfurization absorption tower (12) through a fan inlet pipe (11), the purified flue gas is discharged to a chimney (36) through a top flue gas discharge pipe (35), a dehumidification grid (13), a backwashing pipe (14) with a nozzle, an upper nozzle pipe (16), a separation cover (18) and a lower nozzle pipe (23) are sequentially arranged in the tower from top to bottom along the height, an alkaline solution supply pipe (25) and a branch pipe (26) are respectively connected to the upper nozzle pipe and the lower nozzle pipe so as to spray alkaline solution water downwards from the nozzle, hot flue gas is introduced from one side of the absorption tower through an outlet pipe (11) of a fan (10) and flows upwards from bottom to be uniformly mixed with the sprayed alkaline solution water, desulfurization reaction is carried out in an upper spraying absorption area (15), and oxidation reaction is carried out in a lower oxidation area (24), in order to improve the spraying and absorption efficiency, an upper circulating pump (20) is arranged, an inlet pipeline of the upper circulating pump is connected with a liquid storage tank (19) and stores the solution discharged from the upper part of the separation cover (18), an outlet pipeline of the upper circulating pump is connected with a recirculation pipe (21) to realize the recirculation of the solution, and the other part of the upper circulating pump is connected with an upper liquid discharge pipe (22) and is connected with a lower nozzle pipe (23) to discharge the solution to the lower part. The sulfate solution (27) flowing to the bottom of the tower is connected with a lower nozzle pipe (23) through a recirculation pipe (30) by a lower circulation pump (29) to realize lower solution recirculation, the other part of byproduct solution is communicated with a concentration tank (32) through a discharge pipe (31) to be dehydrated, and then is discharged to an evaporator (3) through a concentration liquid pump (34), is sprayed out from a nozzle on a nozzle pipe (2) and is supplied with the smoke from a hot smoke inlet pipe (1) entering from the upper part or introduced heat auxiliaryThe source (37) is contacted to evaporate the aqueous solution to dryness and to feed it through the bottom evaporator outlet (4) to a bag collector (5) equipped with a filter bag (7) where the solid particles of the by-product, i.e. Na, are separated from the flue gas2SO4Or MgSO 24And is discharged from a byproduct discharge pipe (8). The discharged flue gas and the other path of hot flue gas which is not desulfurized are connected and mixed with a fan inlet pipe (6) through a hot flue gas inlet branch pipe (9), and are led into an absorption tower (12) through a fan (10), and the acid gas removed from the flue gas is discharged through a smoke discharge pipe (35) and a chimney (36). The separating cover (18) can be one or a combination of a plurality of separating covers. The back-flushing pipe (14) with nozzles, the uppernozzle pipe (16) and the lower nozzle pipe (23) can be respectively arranged in one row or more than two rows in the absorption tower (12), and a plurality of branch pipes with nozzles are separated from each row in the absorption tower and distributed on the same plane. The tower may or may not be filled with packing (17) or other systems for mixing flue gas with spray liquid, and the lower part of the tower is provided with an air pipe (28) for supplying air for solution oxidation. A return pipe (33) is installed at one side of the upper part of the concentration tank (32) so as to return water to the system.
The procedure of the desulfurization reaction was:
the desulfurization reaction with magnesium base in the absorption tower is:
the oxidation reaction carried out at the lower part of the absorption tower is as follows:
the product is a mixture of solution and suspension, and is fed into a thickener to remove part of water and increase concentration
And finally, completely drying in an evaporator.
Or using a sodium based desulfurizing agent such as sodium hydroxide (NaOH):
and (3) oxidation reaction:
the product is sulfate solution, or directly sent to a water evaporator to be dried by smoke gas, and the water solution is evaporated to dryness. The evaporated by-product and the exhaust gas mixture are sent to a collector to separate the by-product solid particles from the flue gas flow, and the by-product is the dry state Na2SO4Or MgSO 24And the flue gas is taken as exhaust gas and sent to an absorption tower.
Claims (5)
1. The utility model provides a sodium-based or magnesium-based wet flue gas desulfurization system of no waste of complete recovery accessory substance, it includes cask shape desulfurization absorption tower (12), concentration jar (32), evaporimeter (3), filter bag formula collector (5), fan (10) and circulating pump (20, 29), its characterized in that: a flue gas discharge pipe (35) is arranged at the top of the barrel-shaped desulfurization absorption tower (12), a dehumidification grid (13), a backwashing pipe (14) with a nozzle, an upper nozzle pipe (16), a separation cover (18) and a lower nozzle pipe (23) are sequentially arranged in the tower from top to bottom along the height, an alkaline solution supply main pipe (25) and a branch pipe (26) are arranged at one side of the tower and are respectively connected to the upper nozzle pipe (16) and the lower nozzle pipe (23), so that the provided alkaline solution is sprayed downwards from the nozzle, the fluegas passes through a fan outlet pipe (11) and is introduced into the lower part of the tower and forms reverse flow and mixing with the spray liquid from bottom to top, the desulfurization reaction and the oxidation reaction are carried out in an upper spray absorption area (15) and a lower oxidation area (24), the upper desulfurization product is discharged to a liquid storage tank (19), returns to the upper nozzle pipe (16) through an upper circulating pump (20) and a recycling pipe (21) and is discharged to the lower nozzle pipe (23) through an upper liquid, the oxidation reaction is carried out in a lower oxidation zone (24). The sulfate solution (27) of the reaction product flows to the lower part of the tower, returns to a lower nozzle pipe (23) through a recirculation pipe (30) by a lower circulating pump (29), meanwhile, the sulfate solution (27) is sent to a concentration tank (32) through a discharge pipe (31), is sent to an evaporator (3) by a concentration liquid pump (34) after dehydration, is sprayed out from the nozzle pipe (2), hot flue gas is sent to the upper part of the evaporator (3) from top to bottom through a hot flue gas inlet pipe (1) or other auxiliary heat sources (37), is mixed with the sulfate solution sprayed out from the nozzle pipe (2), water in the solution is evaporated and dried, and is sent to a filter bag type collector (5) through an evaporator outlet pipe (4) at the lower part, solid particles in the by-product are separated from the flue gas, namely, the by-product finished product is obtained and discharged through a by-product discharge tank (8), and the flue gas discharged from the collector (5) is mixed with unpurified flue gas (9) and sent to the lower part of an absorption tower (12) by a fan (10) .
2. The sodium-based or magnesium-based wet flue gas desulfurization system of claim 1, wherein: the separating cover (18) can be one or a plurality of combinations.
3. The sodium-based or magnesium-based wet flue gas desulfurization system of claim 1, wherein: the back-flushing pipe (14) with nozzles, the upper nozzle pipe (16) and the lower nozzle pipe (23) can be respectively arranged in a row or more than two rows in the absorption tower (12), and a plurality of branch pipes with nozzles are separated from each row in the absorption tower and distributed on the same plane.
4. The sodium-based or magnesium-based wet flue gas desulfurization system of claim 1, wherein: the byproduct salt solution discharged from the desulfurization absorption tower (12) can pass through a byproduct solution discharge pipe (31) to pass through a concentration tank (32) to remove part of moisture and then be dried in an evaporator (3), or the solution can directly enter the evaporator (3) to be dried without the concentration tank (32), and then the dry desulfurization byproduct obtained by a collector (5) is discharged through a byproduct discharge pipe (8).
5. The sodium-based or magnesium-based wet flue gas desulfurization system of claim 1, wherein: the desulfurization absorption tower (12) is composed of an upper desulfurization spraying area (15) and a lower oxidation area (24), wherein the upper desulfurization spraying area can be filled with a filler (17) or not, or other replacing systems for mixing downward spraying liquid and upward flue gas are adopted.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01144928 CN1428186A (en) | 2001-12-24 | 2001-12-24 | Sodium base or magnesium base wet flue gas desulfurizing system capable of completely recovering by-product without wastes |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01144928 CN1428186A (en) | 2001-12-24 | 2001-12-24 | Sodium base or magnesium base wet flue gas desulfurizing system capable of completely recovering by-product without wastes |
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| Publication Number | Publication Date |
|---|---|
| CN1428186A true CN1428186A (en) | 2003-07-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01144928 Pending CN1428186A (en) | 2001-12-24 | 2001-12-24 | Sodium base or magnesium base wet flue gas desulfurizing system capable of completely recovering by-product without wastes |
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|---|---|
| CN (1) | CN1428186A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836629A (en) * | 2012-09-07 | 2012-12-26 | 王中位 | Flue gas desulfurization dust removal process and apparatus |
| CN103341274A (en) * | 2013-07-10 | 2013-10-09 | 北京国电龙源环保工程有限公司 | Device and method for moisture recovery and gypsum rain control in wet desulphurization flue gas of thermal power plant |
| CN103697551A (en) * | 2013-12-18 | 2014-04-02 | 山东科技大学 | Indoor semiconductor cooling and dehumidification device |
| CN107511075A (en) * | 2017-08-21 | 2017-12-26 | 哈尔滨工程大学 | A kind of new spray column removes ship tail gas NO simultaneouslyxAnd SO2Device and method |
| CN108744565A (en) * | 2018-07-31 | 2018-11-06 | 中国大唐集团科学技术研究院有限公司西北分公司 | A kind of evaporative crystallization heat-exchanger rig and coal fired plant desulfurization wastewater Zero discharging system |
| CN110090550A (en) * | 2019-04-17 | 2019-08-06 | 昆明理工大学 | A kind of coke oven flue gas sulfur method thermally decomposed in advance based on magnesium salts |
-
2001
- 2001-12-24 CN CN 01144928 patent/CN1428186A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836629A (en) * | 2012-09-07 | 2012-12-26 | 王中位 | Flue gas desulfurization dust removal process and apparatus |
| CN103341274A (en) * | 2013-07-10 | 2013-10-09 | 北京国电龙源环保工程有限公司 | Device and method for moisture recovery and gypsum rain control in wet desulphurization flue gas of thermal power plant |
| CN103341274B (en) * | 2013-07-10 | 2016-03-02 | 北京国电龙源环保工程有限公司 | In heat-engine plant wet desulfurization fume, moisture reclaims and gypsum rain controlling device and method |
| CN103697551A (en) * | 2013-12-18 | 2014-04-02 | 山东科技大学 | Indoor semiconductor cooling and dehumidification device |
| CN103697551B (en) * | 2013-12-18 | 2018-11-20 | 山东科技大学 | A kind of interior semiconductor cooling dehumidification device |
| CN107511075A (en) * | 2017-08-21 | 2017-12-26 | 哈尔滨工程大学 | A kind of new spray column removes ship tail gas NO simultaneouslyxAnd SO2Device and method |
| CN107511075B (en) * | 2017-08-21 | 2020-10-27 | 哈尔滨工程大学 | Spray tower simultaneously removes boats and ships tail gas NOxAnd SO2Method (2) |
| CN108744565A (en) * | 2018-07-31 | 2018-11-06 | 中国大唐集团科学技术研究院有限公司西北分公司 | A kind of evaporative crystallization heat-exchanger rig and coal fired plant desulfurization wastewater Zero discharging system |
| CN108744565B (en) * | 2018-07-31 | 2023-07-14 | 中国大唐集团科学技术研究院有限公司西北分公司 | Evaporation crystallization heat exchange device and desulfurization wastewater zero discharge system of coal-fired plant |
| CN110090550A (en) * | 2019-04-17 | 2019-08-06 | 昆明理工大学 | A kind of coke oven flue gas sulfur method thermally decomposed in advance based on magnesium salts |
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