CN102976285A - Method for preparing sulfuric acid from desulfurized gypsum in secondary lead smelting process as raw material - Google Patents
Method for preparing sulfuric acid from desulfurized gypsum in secondary lead smelting process as raw material Download PDFInfo
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- CN102976285A CN102976285A CN2012105083374A CN201210508337A CN102976285A CN 102976285 A CN102976285 A CN 102976285A CN 2012105083374 A CN2012105083374 A CN 2012105083374A CN 201210508337 A CN201210508337 A CN 201210508337A CN 102976285 A CN102976285 A CN 102976285A
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Abstract
The invention discloses a method for preparing sulfuric acid from desulfurized gypsum in a secondary lead smelting process as a raw material. The method comprises the following steps of: (a) taking desulfurized gypsum waste residue in the secondary lead smelting process, dewatering and then baking the desulfurized gypsum waste residue; (b) adding pulverized coal and an additive to the baked desulfurized gypsum, crushing and grinding to form an even mixture, burning and decomposing the desulfurized gypsum after pre-heating, carrying out high-temperature oxidation reaction on product high-temperature SO2 smoke after dust removal and oxygen enrichment, and carrying out heat exchange on the mixed gas to dry the desulfurized gypsum waste residue; (c) reducing the temperature of the heat-exchanged mixed gas, carrying out oxygen-enriched oxidation on the mixed gas again under the condition that a catalyst V2O5 exists; and (e) absorbing the obtained SO3 gas by concentrated sulfuric acid. The sulfuric acid is prepared from the desulfurized gypsum waste residue in the secondary lead smelting process; and the problem of difficulty in processing the desulfurized gypsum is solved, and rubbish is reused, and meanwhile, domestic sulfur resources are saved.
Description
Technical field
The method that the present invention relates to utilize the desulfurated plaster waste residue in the secondary lead smelting process to produce sulfuric acid belongs to the comprehensive utilization of industry by-product gypsum residue resource and enviromental protection and improvement field.
Background technology
The annual industrially desulfurized gypsum quantity discharged of China surpasses 7,000 ten thousand tons at present, and along with country was to the increasing of flue gas desulfurization management in recent years, the quantity discharged of desulfurated plaster will rise rapidly.Because the industry by-product gypsum fineness is high, and is moisture many, contains objectionable impurities, have influence on it and can utilize degree, any discharging can cause serious environmental pollution, and the landfill occupation of land is many, and investment is large, and long-term accumulation meeting pollutes environment and water quality on every side.
The method of traditional technology extracting sulfuric acid generally adopts the high-temperature roasting containing sulfur minerals, at first obtains SO
2The flue gas that gas content is larger is with changing at last SO by a series of equipment such as gas dust remover, cooling tower, circulating washing tower, gas condenser, electrostatic precipitator, drying tower, oxidation furnaces, gas heat exchangers
3, be absorbed as at last H
2SO
4, this kind method exists operation various, and temperature is high, the large deficiency that waits of environmental pollution; The sulphur that directly burns in addition, but also extracting sulfuric acid, but the same waste resource that exists, the shortcoming such as operation is various.
The technical study of gypsum extracting sulfuric acid started from for 20 beginnings of the century, and China has made more advanced, the larger device of gypsum relieving haperacidity technology on the basis of summing up domestic and international technology.But it exists hear rate large, and power consumption is large, and investment is high, the shortcoming of deficiency in economic performance, although after this a lot of modifying devices and technique are arranged, fluctuation of service, cost of investment is high, easily causes secondary pollution problems still effectively not solved.
Summary of the invention
The objective of the invention is in order to make the desulfurated plaster waste residue in the secondary lead smelting process can access re-using; solve the practical problems of factory; be beneficial to environment protection; provide that a kind of cost is low, energy consumption is little, production unit succinctly, almost free of contamination desulfurated plaster in the secondary lead smelting process is the method for waste sulfuric acid, by product calcium oxide recycling capable of circulation simultaneously.
Technical scheme of the present invention is as follows:
A kind of desulfurated plaster in the secondary lead smelting process is the method for waste sulfuric acid, may further comprise the steps:
(a) get desulfurated plaster waste residue in the secondary lead smelting process, the dehydration post-drying;
(b) add coal dust and additive in the desulfurated plaster after the oven dry, become uniform compound behind the crushing and grinding, calcining and decomposing desulfurated plaster after the preheating, product high temperature SO
2Behind the flue gas process dedusting oxygen enrichment, carry out the high temperature oxidation reaction, mixed gas is used for the oven dry of desulfurated plaster waste residue by heat exchange;
(c) reduce through mixed gas temperature after the heat exchange, catalyst V is being arranged
2O
5Under the condition that exists, mixed gas is carried out oxygen-rich oxide again;
(e) SO that obtains
3Gas absorbs with the vitriol oil.
Further, described additive is Fe
2O
3, Fe
3O
4Or its combination.
Further, the weight ratio of desulfurated plaster, coal dust and additive is 100:(10～25 in the described step (b)): (1～5).
Further, the granularity of compound is 1～5mm described in the described step (b), and calcining temperature is 800～950 ℃, and calcination time is 6～15min; The temperature of high temperature oxidation reaction is 500～700 ℃.
Further, the temperature in the described step (c) is 150～200 ℃.
Further, adopt Aerodynamic Inverse to gas absorbing device in the described step (e).
Further, Aerodynamic Inverse mainly comprises the sour pond of storage, recycle pump, booster fan, surge chamber, membrane filtration chamber, absorption chamber, steam separator and former gas flue to gas absorbing device, and the side of described surge chamber is provided with SO
3Be connected by pipeline between the gas inlet, booster fan and surge chamber, the top of surge chamber is followed successively by membrane filtration chamber, absorption chamber, steam separator; Be connected by pipeline between steam separator and the former gas flue, be connected by pipeline between described steam separator and the sour pond of storage, the sour pond of described storage is connected to absorption chamber by recycle pump and pipeline, and the sour pond of described storage is arranged on below the surge chamber and by pipeline and connects.
Further, Aerodynamic Inverse SO in the gas absorbing device
3The oblique angle that gas enters surge chamber is 10～45 °.
Among the present invention, the correlated response equation:
CaSO
4?+?2C?=?CaS?+?2CO
2
CaS?+?3CaSO
4?=?4CaO?+?4?SO
2
2CaSO
4?+?C?=?2CaO?+?2?SO
2?+?CO
2
2SO
2+O
2=?2SO
3
H
2SO
4?+SO
3?=?H
2S
2O
7
Compared with prior art, the present invention has following beneficial effect:
1) for solving difficult this problem of secondary lead smelting desulfurated plaster waste residue; respond simultaneously national save energy; the call of protection of the environment, the application provides the method for a kind of desulfurated plaster in the secondary lead smelting process as waste sulfuric acid, simultaneously by product calcium oxide recycling capable of circulation.Utilize the desulfurated plaster waste residue in the secondary lead smelting process to come extracting sulfuric acid, not only solved the intractable problem of desulfurated plaster, refuse is utilized again, saved simultaneously domestic sulphur resource.
2) oven dry of desulfurated plaster has been adopted and high temperature SO
2Flue gas carries out the method for heat exchange, has simplified equipment configuration, has reduced input cost.
3) coal dust and additive metal oxide (are mainly Fe
2O
3, Fe
3O
4) adding, reduced the decomposition temperature of calcium sulfate in the desulfurated plaster waste residue, solve simultaneously the agglomeration problems in the calcination process.
4) adopt high and low temperature flue gas secondary oxygen-rich oxide technique, prolonged SO
2Oxidization time, SO
2Be converted into SO
3Transformation efficiency reach more than 98%.
5) the by product calcium oxide after the roasting can directly be sent into the slurrying continuation recycling of slurrying pond, and last tail gas is incorporated the former gas flue of secondary lead factory thionizer into, has avoided the secondary pollution problem.
6) SO
3Adopt Aerodynamic Inverse to SO
3Gas absorbing device absorbs, and has improved greatly SO
3Assimilated efficiency.
Description of drawings
Fig. 1 is process flow sheet of the present invention;
Fig. 2 is that Aerodynamic Inverse is to SO
3The synoptic diagram of gas absorbing device;
Among the figure, 1 is the sour pond of storage, and 2 is recycle pump, and 3 is booster fan, and 4 is surge chamber, and 5 is the membrane filtration chamber, and 6 is absorption chamber, and 7 is steam separator, and 8 is former gas flue.
Embodiment
Below in conjunction with the drawings and specific embodiments, the desulfurated plaster of further setting forth among the present invention in the secondary lead smelting process is the method for waste sulfuric acid, also illustrates simultaneously to be used for SO among the present invention
3The device that absorbs.These examples only are not used in for explanation the present invention and limit the scope of the invention.Not marked experimental technique in the following example is according to normal condition.
A kind of method for preparing sulfuric acid, the concrete technology flow process is as follows:
1) gets a certain amount of secondary lead smelting desulfurated plaster waste residue, send into vacuum belt dewaterer and dewater, obtain the desulfurated plaster waste residue of moisture content below 12%.
2) the desulfurated plaster waste residue is sent into flash drying machine via conveyor and is dried.Because of the SO after the gypsum decomposition in next step
2Gas temperature is very high, by being used for the oven dry of desulfurated plaster waste residue after the heat exchange.
3) add a certain amount of coal dust and additive in the gypsum after the oven dry, the effect Main Function of coal dust is the decomposition temperature that reduces gypsum, the effect of additive is the decomposition temperature that reduces gypsum, prevent from becoming even compound behind the cake broke grinding in the calcination process, control compound granularity is at 1～5mm, can decompose 800～950 ℃ of lower calcinings after the preheating, calcination time 6～15min, it is for subsequent use that by product (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying, and temperature reaches 500～700 ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.
4) (be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after high low temperature secondary oxygen-rich oxide reaction, SO
2Be converted into SO
3Transformation efficiency greatly improve.
5) SO that obtains
3Be with 60 ℃, 98% the vitriol oil adopts Aerodynamic Inverse to absorb to gas absorbing device.SO
3Gas enters from surge chamber 4 lower ends at a certain angle, through passing through membrane filtration chamber 5 after booster fan 3 pressurizations, and with collide at absorption chamber 6 from the vitriol oil absorption liquid that flows down, gas high speed rotary-cut absorption liquid, gas-liquid two-phase continues mutually, and collision fully mixes, form the solution of similar emulsion layer and can continue and keep the formation absorption layer.In the absorption process, the absorption liquid of storing in the sour pond 1 constantly injects absorption chamber 6 via recycle pump 2, along with absorption liquid in the absorption chamber 6 increases, absorbs a large amount of SO in the previous absorption layer that forms
3Gas absorption liquid just flows into the sour pond 1 of storage, and the tail gas after the absorption is incorporated former gas flue 8 into.As long as guarantee SO
3Airshed, the vitriol oil just can continue to absorb SO
3Gas.This kind method has improved SO greatly
3Assimilated efficiency.
6) last tail gas has been avoided the possibility of secondary pollution through incorporating the former flue gas flue of thionizer behind the steam separator 7 into.
The vacuum belt dewaterer of learning from else's experience dehydration, the desulfurated plaster waste residue 400kg after the flash drying machine oven dry adds 80kg coal dust and 5kg additive Fe
2O
3Become even compound behind the crushing and grinding, control compound granularity is at 1～3mm, and at 950 ℃ of lower calcining 15min, it is for subsequent use that the by product that obtains (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying after the preheating, and temperature reaches 500～700 ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.(be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be down to 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after the reaction of high and low temperature secondary oxygen-rich oxide, the SO that obtains
3With 60 ℃, 98% the vitriol oil adopts pneumatic reversing device to absorb.SO after the pressure
3Gas is with 10
oThe pitch angle enters from the surge chamber lower end.The former flue gas flue of incorporating thionizer after last tail gas separates through carbonated drink into.Making 98% the vitriol oil in the present embodiment is 269kg.
Embodiment 2
The vacuum belt dewaterer of learning from else's experience dehydration, the desulfurated plaster waste residue 400kg after the flash drying machine oven dry adds 40kg coal dust and 4kg additive Fe
3O
4Become even compound behind the crushing and grinding, control compound granularity is at 1～3mm, and at 800 ℃ of lower calcining 10min, it is for subsequent use that the by product that obtains (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying after the preheating, and temperature reaches 500～700 ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.(be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be down to 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after high low temperature secondary oxygen-rich oxide reaction, the SO that obtains
3With 60 ℃, 98% the vitriol oil adopts pneumatic reversing device to absorb.SO after the pressure
3Gas is with 20
oThe pitch angle enters from the surge chamber lower end.The former flue gas flue of incorporating thionizer after last tail gas separates through carbonated drink into.Making 98% the vitriol oil in the present embodiment is 257kg.
The vacuum belt dewaterer of learning from else's experience dehydration, the desulfurated plaster waste residue 400kg after the flash drying machine oven dry adds 100kg coal dust, 10kg additive Fe
2O
3And 10kg additive Fe
3O
4Become even compound behind the crushing and grinding, control compound granularity is at 3～5mm, and at 850 ℃ of lower calcining 6min, it is for subsequent use that the by product that obtains (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying after the preheating, and temperature reaches 500～700 ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.(be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be down to 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after high low temperature secondary oxygen-rich oxide reaction, the SO that obtains
3With 60 ℃, 98% the vitriol oil adopts pneumatic reversing device to absorb.SO after the pressure
3Gas is with 30
oThe pitch angle enters from inhaling the surge chamber lower end.The former flue gas flue of incorporating thionizer after last tail gas separates through carbonated drink into.Making 98% the vitriol oil in the present embodiment is 286kg.
Embodiment 4
The vacuum belt dewaterer of learning from else's experience dehydration, the desulfurated plaster waste residue 400kg after the flash drying machine oven dry adds 60kg coal dust and 14kg additive Fe
2O
3Become even compound behind the crushing and grinding, control compound granularity is at 3～5mm, and at 900 ℃ of lower calcining 8min, it is for subsequent use that the by product that obtains (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying after the preheating, and temperature reaches 500～700 ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.(be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be down to 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after high low temperature secondary oxygen-rich oxide reaction, the SO that obtains
3With 60 ℃, 98% the vitriol oil adopts pneumatic reversing device to absorb.SO after the pressure
3Gas is with 45
oThe pitch angle enters from the surge chamber lower end.The former flue gas flue of incorporating thionizer after last tail gas separates through carbonated drink into.Making 98% the vitriol oil in the present embodiment is 263kg.
The vacuum belt dewaterer of learning from else's experience dehydration, the desulfurated plaster waste residue 400kg after the flash drying machine oven dry adds 80kg coal dust and 20kg additive Fe
2O
3Become even compound behind the crushing and grinding, control compound granularity is at 1～3mm, and at 800 ℃ of lower calcining 12min, it is for subsequent use that the by product that obtains (being mainly calcium oxide) directly returns thionizer slurrying pond slurrying after the preheating, and temperature reaches 500～700 ℃ ℃ product S O
2Carry out heat exchange process after the reaction of flue gas ash removal oxygen enrichment, be used for the oven dry of desulfurated plaster waste residue.(be mainly and contain SO through mixed gas after the heat exchange
2, SO
3, O
2) temperature be down to 150～200 ℃, catalyst V is being arranged
2O
5Under the condition that exists, low-temperature mixed gas is carried out oxygen-rich oxide again, after high low temperature secondary oxygen-rich oxide reaction, the SO that obtains
3With 60 ℃, 98% the vitriol oil adopts pneumatic reversing device to absorb.SO after the pressure
3Gas is with 35
oThe pitch angle enters from the surge chamber lower end.The former flue gas flue of incorporating thionizer after last tail gas separates through carbonated drink into.Making 98% the vitriol oil in the present embodiment is 277kg.
Claims (8)
1. the desulfurated plaster in the secondary lead smelting process is the method for waste sulfuric acid, it is characterized in that may further comprise the steps:
(a) get desulfurated plaster waste residue in the secondary lead smelting process, the dehydration post-drying;
(b) add coal dust and additive in the desulfurated plaster after the oven dry, become uniform compound behind the crushing and grinding, calcining and decomposing desulfurated plaster after the preheating, product high temperature SO
2Behind the flue gas process dedusting oxygen enrichment, carry out the high temperature oxidation reaction, mixed gas is used for the oven dry of desulfurated plaster waste residue by heat exchange;
(c) reduce through mixed gas temperature after the heat exchange, catalyst V is being arranged
2O
5Under the condition that exists, mixed gas is carried out oxygen-rich oxide again;
(e) SO that obtains
3Gas absorbs with the vitriol oil.
2. method according to claim 1 is characterized in that described additive is Fe
2O
3, Fe
3O
4Or its combination.
3. method according to claim 2 is characterized in that: the weight ratio of desulfurated plaster, coal dust and additive is 100:(10～25 in the described step (b)): (1～5).
4. method according to claim 3, it is characterized in that: the granularity of compound is 1～5mm described in the described step (b), and calcining temperature is 800～950 ℃, and calcination time is 6～15min; The temperature of high temperature oxidation reaction is 500～700 ℃.
5. method according to claim 4, it is characterized in that: the temperature in the described step (c) is 150～200 ℃.
6. method according to claim 1 is characterized in that: adopt Aerodynamic Inverse to gas absorbing device in the described step (e).
7. method according to claim 6, it is characterized in that: Aerodynamic Inverse mainly comprises the sour pond of storage, recycle pump, booster fan, surge chamber, membrane filtration chamber, absorption chamber, steam separator and former gas flue to gas absorbing device, and the side of described surge chamber is provided with SO
3Be connected by pipeline between the gas inlet, booster fan and surge chamber, the top of surge chamber is followed successively by membrane filtration chamber, absorption chamber, steam separator; Be connected by pipeline between steam separator and the former gas flue, be connected by pipeline between described steam separator and the sour pond of storage, the sour pond of described storage is connected to absorption chamber by recycle pump and pipeline, and the sour pond of described storage is arranged on below the surge chamber and by pipeline and connects.
8. method according to claim 7 is characterized in that: Aerodynamic Inverse SO in the gas absorbing device
3The oblique angle that gas enters surge chamber is 10～45 °.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210508337.4A CN102976285B (en) | 2012-12-03 | 2012-12-03 | Method for preparing sulfuric acid from desulfurized gypsum in secondary lead smelting process as raw material |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210508337.4A CN102976285B (en) | 2012-12-03 | 2012-12-03 | Method for preparing sulfuric acid from desulfurized gypsum in secondary lead smelting process as raw material |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108996481A (en) * | 2018-07-16 | 2018-12-14 | 超威电源有限公司 | A kind of lead plaster doctor solution circulation utilization method |
| CN115006982A (en) * | 2022-01-18 | 2022-09-06 | 昆明理工大学 | Method for desulfurizing and carbon-fixing coal-fired flue gas by using carbide slag slurry |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1993001125A1 (en) * | 1991-07-03 | 1993-01-21 | Radian Corporation | Cocurrent scrubber method and system |
| CN1724338A (en) * | 2005-06-16 | 2006-01-25 | 什邡市鸿升化工有限公司 | Process for producing industrial sulfuric acid using phosphorus gypsum as raw material |
| CN1958498A (en) * | 2006-11-24 | 2007-05-09 | 湖南永清脱硫有限公司 | Method for producing cement and vitriol from desulfurized gesso of flue gas |
| KR20090032569A (en) * | 2007-09-28 | 2009-04-01 | 한국전력공사 | Method for improvement of brightness of fgd gypsum using sulfuric acid and gypsum seed |
| CN101708421A (en) * | 2009-11-16 | 2010-05-19 | 浙江大学 | Device and method for removing various pollutants simultaneously by lime stone-gypsum wet process |
| CN101891160A (en) * | 2010-06-21 | 2010-11-24 | 尹小林 | Method for directly preparing sulfur trioxide and sulfuric acid from plaster |
| CN102515115A (en) * | 2011-12-29 | 2012-06-27 | 刘立文 | Method for preparing sulfuric acid and cement by using desulfurized gypsum |
| CN102716657A (en) * | 2012-06-13 | 2012-10-10 | 河南豫光锌业有限公司 | Zinc oxide desulfurization method applicable to zinc smelting system |
-
2012
- 2012-12-03 CN CN201210508337.4A patent/CN102976285B/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1993001125A1 (en) * | 1991-07-03 | 1993-01-21 | Radian Corporation | Cocurrent scrubber method and system |
| CN1724338A (en) * | 2005-06-16 | 2006-01-25 | 什邡市鸿升化工有限公司 | Process for producing industrial sulfuric acid using phosphorus gypsum as raw material |
| CN1958498A (en) * | 2006-11-24 | 2007-05-09 | 湖南永清脱硫有限公司 | Method for producing cement and vitriol from desulfurized gesso of flue gas |
| KR20090032569A (en) * | 2007-09-28 | 2009-04-01 | 한국전력공사 | Method for improvement of brightness of fgd gypsum using sulfuric acid and gypsum seed |
| CN101708421A (en) * | 2009-11-16 | 2010-05-19 | 浙江大学 | Device and method for removing various pollutants simultaneously by lime stone-gypsum wet process |
| CN101891160A (en) * | 2010-06-21 | 2010-11-24 | 尹小林 | Method for directly preparing sulfur trioxide and sulfuric acid from plaster |
| CN102515115A (en) * | 2011-12-29 | 2012-06-27 | 刘立文 | Method for preparing sulfuric acid and cement by using desulfurized gypsum |
| CN102716657A (en) * | 2012-06-13 | 2012-10-10 | 河南豫光锌业有限公司 | Zinc oxide desulfurization method applicable to zinc smelting system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108996481A (en) * | 2018-07-16 | 2018-12-14 | 超威电源有限公司 | A kind of lead plaster doctor solution circulation utilization method |
| CN115006982A (en) * | 2022-01-18 | 2022-09-06 | 昆明理工大学 | Method for desulfurizing and carbon-fixing coal-fired flue gas by using carbide slag slurry |
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|---|---|
| CN102976285B (en) | 2014-11-19 |
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