CN105502307A - Method for removing fluorine and chlorine from waste acid through concentration and special device - Google Patents
Method for removing fluorine and chlorine from waste acid through concentration and special device Download PDFInfo
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- CN105502307A CN105502307A CN201510982827.1A CN201510982827A CN105502307A CN 105502307 A CN105502307 A CN 105502307A CN 201510982827 A CN201510982827 A CN 201510982827A CN 105502307 A CN105502307 A CN 105502307A
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- Prior art keywords
- acid
- chlorine
- concentration
- fluorine
- tower
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- 239000002253 acid Substances 0.000 title claims abstract description 100
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000000460 chlorine Substances 0.000 title claims abstract description 74
- 229910052801 chlorine Inorganic materials 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 21
- 229910052731 fluorine Inorganic materials 0.000 title claims abstract description 18
- 239000011737 fluorine Substances 0.000 title claims abstract description 18
- 239000002699 waste material Substances 0.000 title abstract 8
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 title abstract 7
- 238000001704 evaporation Methods 0.000 claims abstract description 58
- 230000008020 evaporation Effects 0.000 claims abstract description 58
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000011593 sulfur Substances 0.000 claims abstract description 6
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 6
- 238000004094 preconcentration Methods 0.000 claims description 25
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 24
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- HXELGNKCCDGMMN-UHFFFAOYSA-N [F].[Cl] Chemical compound [F].[Cl] HXELGNKCCDGMMN-UHFFFAOYSA-N 0.000 claims description 15
- 230000006835 compression Effects 0.000 claims description 12
- 238000007906 compression Methods 0.000 claims description 12
- 230000008676 import Effects 0.000 claims description 12
- 238000000746 purification Methods 0.000 claims description 12
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 claims description 11
- 239000012141 concentrate Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 3
- 239000006200 vaporizer Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 229910052602 gypsum Inorganic materials 0.000 abstract description 4
- 239000010440 gypsum Substances 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 8
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 229910001385 heavy metal Inorganic materials 0.000 description 4
- 235000011149 sulphuric acid Nutrition 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000005987 sulfurization reaction Methods 0.000 description 3
- 239000001117 sulphuric acid Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910052785 arsenic Inorganic materials 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 description 2
- 101100290713 Caenorhabditis elegans mef-2 gene Proteins 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- UXNBTDLSBQFMEH-UHFFFAOYSA-N [Cu].[Zn].[Pb] Chemical compound [Cu].[Zn].[Pb] UXNBTDLSBQFMEH-UHFFFAOYSA-N 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- JZMJDSHXVKJFKW-UHFFFAOYSA-M methyl sulfate(1-) Chemical compound COS([O-])(=O)=O JZMJDSHXVKJFKW-UHFFFAOYSA-M 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- FWFGVMYFCODZRD-UHFFFAOYSA-N oxidanium;hydrogen sulfate Chemical compound O.OS(O)(=O)=O FWFGVMYFCODZRD-UHFFFAOYSA-N 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 235000013024 sodium fluoride Nutrition 0.000 description 1
- 239000011775 sodium fluoride Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/88—Concentration of sulfuric acid
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/90—Separation; Purification
- C01B17/901—Recovery from spent acids containing metallic ions, e.g. hydrolysis acids, pickling acids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a method for removing fluorine and chlorine from waste acid through concentration and a special device. Sulfurized waste acid is subjected to multiple-effect evaporation concentration, and more than 90% of water in the waste acid is evaporated; the concentration of the waste acid during multiple-effect evaporation concentration is controlled to be 25%-40%, the temperature of the waste acid is controlled to be 105-110 DEG C, fluorine and chlorine are still kept in the waste acid, and pre-concentrated acid is obtained; live steam is used for keeping the temperature of the pre-concentrated acid in a reboiler to be 125-145 DEG C, then the pre-concentrated acid enters a fluorine and chlorine removal column, after sulfur separation by multi-stage column plates, fluorine and chlorine in sulfur in the fluorine and chlorine removal column are carried out of the column top along with steam; part of purified acid is taken out of the column bottom, and part of the purified acid still returns to the reboiler. The method for removing fluorine and chlorine from the waste acid through concentration and the special device have the advantages that gypsum residues are avoided, energy consumption can be reduced remarkably, and the device investment is saved.
Description
Technical field
The present invention relates to method and the special purpose device of the sour concentration defluorinating chlorine of a kind of dirt.
Background technology
The flue gas acid preparing process of copper-lead-zinc smelting produces a large amount of acid of the dirt containing heavy metal, and conventional treatment process is sulfuration neutralization.Therefore, produce a large amount of gypsum tailings containing heavy metal, Sulphur ressource is not utilized.In addition, calcic sodium ion in the waste water after process, can not return use substantially.In recent years, domesticly the Technology of dirty acid " sulfuration+hot blast stripping " being is is being researched and developed about manufacturing enterprise.Because dilute sulphuric acid water content is high, the moisture in stripping diluted acid and fluorine chlorine, need a large amount of temperature to be the warm air of 180 DEG C-200 DEG C.So the energy consumption of device is very high.Particularly defluorinate chlorine equipment size is huge, cost is high.And the airstrip acid amount sulfuric acid concentration that is large, that obtain after defluorinate chlorine is low, tail gas treatment device investment is large.In addition, greatly, hot blast stripping device adaptability is poor, operation stability is poor in the dirty acid concentration change that flue gas acid preparing process produces.
Summary of the invention
The object of the present invention is to provide a kind ofly there is no gypsum tailings, significantly can reduce energy consumption, the method for dirt acid concentration defluorinating chlorine that plant investment is economized and special purpose device.
Technical solution of the present invention is:
A method for the sour concentration defluorinating chlorine of dirt, is characterized in that: comprise the following steps:
(1) by after sulfidizing dirt acid concentrated by multiple-effect evaporation, by dirty acid more than 90% moisture evaporation; The concentration controlling dirty acid when multiple-effect evaporation concentrates is 25%-40%, the temperature of the dirty acid of control is 105 DEG C-110 DEG C, fluorine chlorine is still remained in dirty acid, obtains pre-concentration acid; Multiple-effect evaporation concentrates the not fluorine-containing chlorine of water vapor condensation water of generation, can return use;
(2) adopt live steam, in reboiler, the temperature of pre-concentration acid is remained on 125 DEG C-145 DEG C, then pre-concentration acid enters defluorinate chlorine tower, and in defluorinate chlorine tower, the fluorine chlorine in sulfuric acid, after the acid of multistage column plate separate sulfur, is taken out of from tower top with water vapor; Partial cleansing acid taken out at the bottom of tower, Partial cleansing acid still returns reboiler.
The water vapor condensation within the condenser of the fluorine-containing chlorine of defluorinate chlorine top of tower, then delivers to fluorine chlorine recovery system by phlegma.
Described multiple-effect evaporation simmer down to three-effect evaporation and condensation.
A special purpose device for the method for the sour concentration defluorinating chlorine of dirt, is characterized in that: comprise Multi-effect evaporation compression apparatus, arranges defluorinate chlorine device after Multi-effect evaporation compression apparatus; Described Multi-effect evaporation compression apparatus comprises multi-stage evaporation unit, every grade of evaporation unit is composed in series loop by vaporizer, well heater, recycle pump, the gelled acid discharge port of previous stage evaporation unit is communicated with rear stage evaporation unit acid inlet through pumps in series, and the steam outlet of rear stage evaporation unit is communicated with previous stage well heater; Defluorinate chlorine device is led in the pre-concentration acid outlet of last step evaporation unit; The well heater of last step evaporation unit is provided with saturation steam import; Described defluorinate chlorine device comprises preheater, preheater is provided with pre-concentration acid import, the pre-concentration acid outlet of preheater communicates with in the middle part of defluorinate chlorine tower, defluorinate chlorine tower bottom arranges the secondary steam import be connected with reboiler, reboiler is provided with saturation steam import, defluorinate chlorine tower bottom arranges the purification acid first be connected with reboiler and exports, and on reboiler, setting purifies sour outlet with condensed water is tank connected, and the purification acid of condensation water pot exports and is connected with preheater; Defluorinate chlorine tower bottom arranges purification acid second outlet; The steam outlet of defluorinate chlorine top of tower is connected with condenser.
Under certain temperature and certain sulfuric acid concentration, there is following molecular balance in fluorochemical:
MeF2+H2SO4=2HF+MeSO4
As strong acid in one, strong polar molecule HF dissociation degree is in aqueous not high, is mainly present in the aqueous solution with the state of the hydrogen fluoride molecule of free state, and the existence of the vitriol oil further suppress the ionization in aqueous of hydrogen fluoride molecule.But under the state of high temperature highly acidity, hydrogen fluoride molecule can be overflowed whole solution system in the form of a vapor.This process can further increase the entropy of whole system, impels whole molecular balance to move right further, reaches the object of whole system defluorinate.In like manner, hydrogenchloride also will be overflowed in the same manner.
By small-scale test, demonstrate under the condition of relatively low acidity and temperature, hydrogenchloride and hydrogen fluoride molecule cannot remove substantially in the middle of solution system; When sulfuric acid concentration in solution and temperature are enough high, just the most hydrogen fluoride in solution, hydrogenchloride can be removed.But evaporation concentration conveniently, the hydrogen fluoride in sulphuric acid soln, hydrogenchloride decreasing ratio≤80%, return the processing requirement of acid making system after not reaching dirty acid purification.Evaporate the secondary steam water of condensation of generation, fluorine cl content is higher simultaneously, can not Returning utilization.The dirt acid concentration defluorinating chlorine technique of our invention, in the dirt sour pre-concentration stage, by concentration and the temperature of dirty acid during control multiple-effect evaporation, makes fluorine chlorine still remain in dirty acid.The not fluorine-containing chlorine of secondary steam water of condensation that evaporation produces, can return use.Pre-concentration acid after heating up, then enters special defluorinate chlorine device.This device can realize the control and regulation of sulfuric acid concentration and temperature, and is designed with stage trapping column plate, can guarantee the hydrogen fluoride in sulphuric acid soln, hydrogenchloride decreasing ratio is greater than 95%.
Dirty acid, according to conventional processing method, after over cure, clarification, filtration eliminate arsenic and heavy metal, enters dirty sour Multi-effect evaporation compression apparatus.In Multi-effect evaporation compression apparatus, in dirty acid, the moisture content of more than 90% is evaporated.By controlling concentration, the temperature of sulfuric acid, the fluorine chlorine in acid is not separated out, the not fluorine-containing chlorine of secondary steam phlegma.Then, pre-concentration acid enters concentration defluorinating chlorine device.In concentration defluorinating chlorine device, sulfuric acid concentration improves further, temperature improves further, after stage trapping column plate, fluorine chlorine is separated out from solution, and takes system out of with water vapor (secondary steam).Go out the purification acid of concentration defluorinating chlorine device, add as relieving haperacidity the absorption system that water enters sulphuric acid plant, reclaim Sulphur ressource.Water vapor containing fluorine chlorine removes the retrieving arrangement of Sodium Fluoride, sodium-chlor after condensation.
Advantage of the present invention:
1, do not produce gypsum tailings, namely do not produce secondary pollution;
2, dirty acid adopts multiple-effect pre-concentration, and be stripped of the moisture of in dirty acid more than 90%, the not fluorine-containing chlorine of this part steam condensate, can return use;
3, pre-concentration acid defluorinate chlorine equipment adopts " reboiler+defluorinate chlorine tower ", and efficiency is high, equipment size is little, reduced investment, and compared with warm air concentration defluorinating chlorine, energy consumption significantly reduces;
4, dirty acid is after the sulfuration removing heavy metals and arsenic of routine, after multiple-effect evaporation pre-concentration, reboiler defluorinate chlorine, can add acid making system, make Sulphur ressource obtain utilization.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the invention will be further described.
Fig. 1 is Multi-effect evaporation compression apparatus schematic diagram of the present invention.
Fig. 2 is defluorinate chlorine device schematic diagram.
Embodiment
A method for the sour concentration defluorinating chlorine of dirt, comprises the following steps:
(1) by after sulfidizing dirt acid concentrated by multiple-effect evaporation, by dirty acid more than 90% moisture evaporation; The concentration controlling dirty acid when multiple-effect evaporation concentrates is 25%-40%, the temperature of the dirty acid of control is 105 DEG C-110 DEG C, fluorine chlorine is still remained in dirty acid, obtains pre-concentration acid; The not fluorine-containing chlorine of secondary steam water of condensation that evaporation produces, can return use as technique hot water; Multiple-effect evaporation concentrates the not fluorine-containing chlorine of water vapor condensation water of generation, can return use;
(2) adopt live steam, in reboiler, the temperature of pre-concentration acid is remained on 125 DEG C-145 DEG C, then pre-concentration acid enters defluorinate chlorine tower, and in defluorinate chlorine tower, the fluorine chlorine in sulfuric acid, after the acid of multistage column plate separate sulfur, is taken out of from tower top with water vapor; In defluorinate chlorine tower, the fluorine chlorine in sulfuric acid, after the acid of multistage column plate separate sulfur, is taken out of from tower top with water vapor.At the bottom of tower, Partial cleansing acid is taken out, deliver to acid making system or take-away; Partial cleansing acid still returns reboiler.Through this step, the hydrogen fluoride in pre-concentration acid, hydrogenchloride decreasing ratio are more than 95%.Meanwhile, acid is dense carries further to 45%-60%.
The water vapor condensation within the condenser of the fluorine-containing chlorine of defluorinate chlorine top of tower, then delivers to fluorine chlorine recovery system by phlegma.
Described multiple-effect evaporation simmer down to three-effect evaporation and condensation.
A special purpose device for the method for the sour concentration defluorinating chlorine of dirt, comprises Multi-effect evaporation compression apparatus, arranges defluorinate chlorine device after Multi-effect evaporation compression apparatus; Described Multi-effect evaporation compression apparatus comprises multi-stage evaporation unit, every grade of evaporation unit is composed in series loop by vaporizer 1, well heater 2, recycle pump 3, the gelled acid discharge port of previous stage evaporation unit is communicated with rear stage evaporation unit acid inlet through pumps in series 4, and the steam outlet 5 of rear stage evaporation unit is communicated with previous stage well heater; Defluorinate chlorine device is led in the pre-concentration acid outlet of last step evaporation unit; The well heater of last step evaporation unit is provided with saturation steam import 6; Described defluorinate chlorine device comprises preheater 7, preheater is provided with pre-concentration acid import 8, the pre-concentration acid outlet 9 of preheater communicates with the middle part of defluorinate chlorine tower 10, defluorinate chlorine tower bottom arranges the secondary steam import 12 be connected with reboiler 11, reboiler is provided with saturation steam import 13, defluorinate chlorine tower bottom arranges the purification acid first be connected with reboiler and exports 14, reboiler is arranged the purification acid be connected with condensation water pot 15 and exports 16, and the purification acid outlet 17 of condensation water pot is connected with preheater 7; Defluorinate chlorine tower bottom arranges purification acid second outlet 18; The steam outlet 19 of defluorinate chlorine top of tower is connected with condenser 20.Condenser 20 to be provided with in industrial cycle water out 22 under water inlet 21, industrial cycle.
Claims (4)
1. a method for the sour concentration defluorinating chlorine of dirt, is characterized in that: comprise the following steps:
(1) by after sulfidizing dirt acid concentrated by multiple-effect evaporation, by dirty acid more than 90% moisture evaporation; The concentration controlling dirty acid when multiple-effect evaporation concentrates is 25%-40%, the temperature of the dirty acid of control is 105 DEG C-110 DEG C, fluorine chlorine is still remained in dirty acid, obtains pre-concentration acid; Multiple-effect evaporation concentrates the not fluorine-containing chlorine of water vapor condensation water of generation, can return use;
(2) adopt live steam, in reboiler, the temperature of pre-concentration acid is remained on 125 DEG C-145 DEG C, then pre-concentration acid enters defluorinate chlorine tower, and in defluorinate chlorine tower, the fluorine chlorine in sulfuric acid, after the acid of multistage column plate separate sulfur, is taken out of from tower top with water vapor; Partial cleansing acid taken out at the bottom of tower, Partial cleansing acid still returns reboiler.
2. the method for the sour concentration defluorinating chlorine of dirt according to claim 1, is characterized in that: the water vapor condensation within the condenser of the fluorine-containing chlorine of defluorinate chlorine top of tower, then phlegma is delivered to fluorine chlorine recovery system.
3. the method for the sour concentration defluorinating chlorine of dirt according to claim 1, is characterized in that: described multiple-effect evaporation simmer down to three-effect evaporation and condensation.
4. a special purpose device for the method for the sour concentration defluorinating chlorine of dirt according to claim 1, is characterized in that: comprise Multi-effect evaporation compression apparatus, arranges defluorinate chlorine device after Multi-effect evaporation compression apparatus; Described Multi-effect evaporation compression apparatus comprises multi-stage evaporation unit, every grade of evaporation unit is composed in series loop by vaporizer, well heater, recycle pump, the gelled acid discharge port of previous stage evaporation unit is communicated with rear stage evaporation unit acid inlet through pumps in series, and the steam outlet of rear stage evaporation unit is communicated with previous stage well heater; Defluorinate chlorine device is led in the pre-concentration acid outlet of last step evaporation unit; The well heater of last step evaporation unit is provided with saturation steam import; Described defluorinate chlorine device comprises preheater, preheater is provided with pre-concentration acid import, the pre-concentration acid outlet of preheater communicates with in the middle part of defluorinate chlorine tower, defluorinate chlorine tower bottom arranges the secondary steam import be connected with reboiler, reboiler is provided with saturation steam import, defluorinate chlorine tower bottom arranges the purification acid first be connected with reboiler and exports, and on reboiler, setting purifies sour outlet with condensed water is tank connected, and the purification acid of condensation water pot exports and is connected with preheater; Defluorinate chlorine tower bottom arranges purification acid second outlet; The steam outlet of defluorinate chlorine top of tower is connected with condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510982827.1A CN105502307B (en) | 2015-12-24 | 2015-12-24 | The method and special purpose device of waste acid concentration defluorinating chlorine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510982827.1A CN105502307B (en) | 2015-12-24 | 2015-12-24 | The method and special purpose device of waste acid concentration defluorinating chlorine |
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| Publication Number | Publication Date |
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| CN105502307A true CN105502307A (en) | 2016-04-20 |
| CN105502307B CN105502307B (en) | 2017-09-01 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106823759A (en) * | 2017-02-28 | 2017-06-13 | 中国恩菲工程技术有限公司 | Defluorinate chlorine device |
| CN106882777A (en) * | 2017-04-06 | 2017-06-23 | 南通三圣石墨设备科技股份有限公司 | A kind of purifying phosphoric acid concentration technology |
| CN107670315A (en) * | 2017-09-30 | 2018-02-09 | 无锡英罗唯森科技有限公司 | Sulphuric acid concentration system and technique |
| CN109078351A (en) * | 2018-09-17 | 2018-12-25 | 杭州东日节能技术有限公司 | A kind of defluorinate chlorine tower and technique and device using fluorine chlorine in tower removing sulfuric acid |
| CN112387096A (en) * | 2020-10-16 | 2021-02-23 | 楚雄滇中有色金属有限责任公司 | Novel method for purifying and recycling arsenic-containing flue gas by using acidic liquid medium |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106823759A (en) * | 2017-02-28 | 2017-06-13 | 中国恩菲工程技术有限公司 | Defluorinate chlorine device |
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| CN109078351A (en) * | 2018-09-17 | 2018-12-25 | 杭州东日节能技术有限公司 | A kind of defluorinate chlorine tower and technique and device using fluorine chlorine in tower removing sulfuric acid |
| CN109078351B (en) * | 2018-09-17 | 2023-09-05 | 杭州东日节能技术有限公司 | Defluorination chlorine tower and process and device for removing fluorine and chlorine in sulfuric acid by adopting same |
| CN112387096A (en) * | 2020-10-16 | 2021-02-23 | 楚雄滇中有色金属有限责任公司 | Novel method for purifying and recycling arsenic-containing flue gas by using acidic liquid medium |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105502307B (en) | 2017-09-01 |
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Denomination of invention: Method and dedicated device for concentrated defluorination and chlorine removal of polluted acid Granted publication date: 20170901 Pledgee: Bank of Communications Co.,Ltd. Nantong Branch Pledgor: NANTONG SUNSHINE GRAPHITE EQUIPMENT TECHNOLOGY Co.,Ltd. Registration number: Y2024980000877 |
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