CN108164071B - Method for recovering bromine salt from flue gas absorption liquid - Google Patents
Method for recovering bromine salt from flue gas absorption liquid Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 46
- 239000007788 liquid Substances 0.000 title claims abstract description 37
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical class [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 239000003546 flue gas Substances 0.000 title claims abstract description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 10
- 238000006115 defluorination reaction Methods 0.000 claims abstract description 38
- 229910052731 fluorine Inorganic materials 0.000 claims abstract description 31
- 239000011737 fluorine Substances 0.000 claims abstract description 31
- 238000005406 washing Methods 0.000 claims abstract description 16
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 239000002699 waste material Substances 0.000 claims abstract description 6
- 230000001698 pyrogenic effect Effects 0.000 claims abstract description 5
- 238000001704 evaporation Methods 0.000 claims description 24
- 230000008020 evaporation Effects 0.000 claims description 22
- 238000004062 sedimentation Methods 0.000 claims description 17
- 239000006228 supernatant Substances 0.000 claims description 8
- 239000001110 calcium chloride Substances 0.000 claims description 7
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 7
- 230000001276 controlling effect Effects 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 239000000701 coagulant Substances 0.000 claims description 6
- 239000003814 drug Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 239000008394 flocculating agent Substances 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 5
- 238000005345 coagulation Methods 0.000 claims description 5
- 230000015271 coagulation Effects 0.000 claims description 5
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 239000010949 copper Substances 0.000 claims description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 239000011541 reaction mixture Substances 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 claims description 4
- 235000019738 Limestone Nutrition 0.000 claims description 3
- 239000000571 coke Substances 0.000 claims description 3
- 239000000839 emulsion Substances 0.000 claims description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- 239000006028 limestone Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 239000010453 quartz Substances 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 239000004575 stone Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 claims 1
- 238000002156 mixing Methods 0.000 claims 1
- 235000011121 sodium hydroxide Nutrition 0.000 claims 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 abstract description 29
- 239000011575 calcium Substances 0.000 abstract description 10
- 239000003513 alkali Substances 0.000 abstract description 5
- 238000003723 Smelting Methods 0.000 abstract description 4
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 abstract description 4
- 229910052794 bromium Inorganic materials 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 3
- 229910052791 calcium Inorganic materials 0.000 abstract description 3
- 229910052751 metal Inorganic materials 0.000 abstract 1
- 239000002184 metal Substances 0.000 abstract 1
- 150000002739 metals Chemical class 0.000 abstract 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- -1 fluorine ions Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- SHXXPRJOPFJRHA-UHFFFAOYSA-K iron(iii) fluoride Chemical compound F[Fe](F)F SHXXPRJOPFJRHA-UHFFFAOYSA-K 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/583—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing fluoride or fluorine compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
- C02F2101/14—Fluorine or fluorine-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
- Treating Waste Gases (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
A method for recovering bromine salt from flue gas absorption liquid is characterized in that a waste circuit board is used as a main raw material, valuable metals are extracted by adopting a pyrogenic process smelting process, generated flue gas enters a tubular washing tower after pretreatment, washing is carried out by using 30% liquid alkali, and generated washing liquid contains bromine of which the content is as high as 4000 mg/L. The invention adopts a two-stage fluorine removal process, wherein the first stage fluorine removal uses Ca (OH)2‑CaCl2-combined PAM-PAC defluorination; and the second-stage fluorine removal uses a polyferric sulfate-PAM-PAC combined method to remove fluorine. Compared with the conventional wastewater fluorine removal method of removing fluorine and then removing calcium, the method has higher fluorine removal efficiency, controls the fluorine content in the recovered bromine salt to be 0.1 percent or even lower, and effectively improves the quality of the bromine salt.
Description
Technical Field
The invention relates to a method for recovering bromine salt from a flue gas absorption liquid, which mainly takes waste circuit boards and low-grade impure copper as main raw materials, adopts flue gas treated by a pyrogenic process smelting process, and comprehensively removes fluorine from washing liquid generated by liquid alkali absorption, and particularly belongs to the technical field of wastewater treatment.
Background
The method is characterized in that a waste circuit board and low-grade impure copper are mixed as main raw materials, flue gas treated by a pyrometallurgical smelting process is adopted, washing liquid generated by liquid alkali absorption contains sulfur, bromide, fluoride and other components, wherein the concentration of fluorine and bromine is high, the concentration of fluorine is about 300-600 mg/L, the bromine content is 4000mg/L, the recovered bromine in the washing liquid has high economic value, usually, a double-effect evaporation process is adopted to recover bromine salt in the washing liquid, but the washing liquid contains high fluorine ions, so that the bromine salt cannot be directly fed into double-effect evaporation equipment for treatment, otherwise, the equipment is greatly corroded, and the recovered bromine salt quality is influenced by high fluorine content.
The conventional lime defluorination and calcium removal process is influenced by the pH value, when the pH value is more than 10, the defluorination efficiency is obviously reduced, and the lime defluorination is repeatedly carried out after the PH value is adjusted back. The invention is realized by a section of Ca (OH)2-CaCl2The fluorine removal by the PAM-PAC combined method solves the problem, and the further fluorine removal by the polyferric sulfate-PAM-PAC combined method at the second stage solves the problem that the PH value is adjusted back to F and is continuously increased.
Disclosure of Invention
The invention aims to remove high-content fluorine from the recovered washing liquid and ensure the quality of bromine salt. The fluorine content in the washing liquid is reduced by improving the pretreatment process of the washing liquid, and the treated washing liquid enters a double-effect evaporation system, so that double-effect evaporation equipment can be protected, and the quality of bromine salt can be effectively improved. Compared with the conventional calcium removal process after lime fluorine removal, the process is better, and the fluorine content of the bromine salt can be reduced to be below 0.1 percent.
A process for recovering bromine salt from the washed liquid of fume includes such steps as absorbing the waste gas containing bromide, fluoride and chloride with 30% liquid alkali to generate an absorption liquid containing bromide, chloride and fluoride, delivering the washed liquid to the pre-treating system of washed liquid, delivering the supernatant to dual-effect evaporating regulating pool, filtering by plate-frame liquid press, and pumping it to dual-effect evaporating system. The pretreatment is mainly to remove fluoride in the washing liquid, and the steam used by the double-effect evaporation system comes from a waste heat boiler.
The method comprises the following steps:
the flue gas is generated by using waste circuit boards and low-grade impure copper as main raw materials and limestone, quartz stone and coke as auxiliary materials through pyrogenic process treatment.
The absorption liquid is subjected to defluorination pretreatment, a two-stage defluorination method is adopted, and a first-stage defluorination process comprises the following steps: using Ca (OH)2-CaCl2Removing fluorine by using a PAM polyacrylamide-PAC polyaluminium chloride combination method; two-stage defluorination process: fluorine removal is carried out by using a polymeric ferric sulfate-PAM-PAC combined method.
A first-stage defluorination process: using Ca (OH)2-CaCl2PAM-PAC combinations using Ca (OH)2-CaCl2And (4) removing by a PAM-PAC combined method, conveying the washed liquid to a first-stage defluorination reaction tank, adding lime emulsion, and controlling the pH value to be 10.0.
Adding CaCl2The amount of the solution added is the Ca content of the coagulated solution2+The content is 45-50 mg/L. PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L. Controlling the solution to coagulate and react for 25-30 min, and then putting the solution into a first-stage defluorination sedimentation tank for natural sedimentation.
And after the natural settling time of the solution in the first-stage defluorination settling tank is more than or equal to 5.0 hours, performing second-stage defluorination.
Two-stage defluorination process: the fluorine is removed by using a polymeric ferric sulfate-PAM-PAC combined method, and the two-stage fluorine removal process also adopts an intermittent treatment mode.
The possible reactions of polymeric ferric sulphate with fluoride ions are as follows:
Fe3++6F-＝FeF6 3-Fe3++5F-＝FeF5 2-
Fe3++4F-＝FeF4 -Fe3++3F-＝FeF3
conveying the supernatant of the first-stage defluorination sedimentation tank to a second-stage defluorination reaction tank, and adding acid (HCl or H) after the tank is full2SO4) Adjusting the pH value to 6.0-7.5, and stirring for 3-5 min.
And after the reaction is finished, adding a polymeric ferric sulfate solution, wherein the adding amount is 450-500 mg/L. PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L. And controlling the coagulation and reaction time for 25-30 min, and then placing the mixture into a two-stage defluorination sedimentation tank for natural sedimentation.
And after the natural settling time of the solution in the second-stage defluorination settling tank is more than or equal to 5.0 hours, conveying the supernatant of the settling tank to a double-effect evaporation regulating tank, filtering by a plate-frame type hydraulic press, and then feeding into a double-effect evaporation system by a feeding pump.
The steam required by the double-effect evaporation system is generated by a waste heat boiler and is conveyed through a pipeline to evaporate the heat required by salt.
The invention has the beneficial effects that:
the invention recovers the bromine salt through double-effect evaporation after the two-stage defluorination pretreatment of the washed liquid, obviously reduces the corrosive damage of the washed liquid to double-effect evaporation equipment, ensures that the fluorine content in the recovered bromine salt is lower than 0.1 percent, effectively improves the quality of the bromine salt, reduces the discharge of waste water while realizing the reutilization of effective components in the waste water, and is beneficial to the environmental protection.
Drawings
FIG. 1 is a schematic view of the process of the present invention.
Detailed Description
Example 1
The method comprises the steps of carrying out pyrogenic smelting by using waste circuit boards and low-grade impure copper as main raw materials and limestone, quartz stone and coke as auxiliary materials, passing smelted flue gas through a high-efficiency pipeline type reaction desulfurizing tower, and obtaining acidic Substances (SO) in the flue gas2HBr, HCl, HF, etc.) is dissolved in the lye sprayed from the top of the desulfurization tower. The alkali liquor with dissolved acid substances circulates in the desulfurizing tower, and the washing liquid is obtained when the concentration of the concentrated solution reaches the discharge set value.
The washing liquid contains 300-600 mg/L of fluorine, the fluorine content in the wastewater passing through the first-stage fluorine removal reaction tank is 40-50 mg/L, the fluorine removal efficiency is up to 90%, and the effect is very obvious.
And (3) through a two-stage defluorination process, further reducing the fluorine content in the washed liquid to 25-40 mg/L, conveying the treated supernatant to a double-effect evaporation regulating pool, filtering by a plate-frame type hydraulic press, and then feeding into a double-effect evaporation system by a feeding pump. The steam used by the double-effect evaporation system is sourced from a waste heat boiler. The fluorine content in the recovered bromine salt is lower than 0.1 percent, and all heavy metals are far less than the 'hazardous waste identification Standard leaching toxicity identification' (GB)
5085-.
The first stage defluorination process comprises the following steps: delivering the washed solution to a first-stage defluorination reaction tank, adding lime emulsion to control the pH to be 10.0, and then adding CaCl2The amount of the added solution is the Ca in the coagulated solution2+The content is 50 mg/L; PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L; controlling the solution to coagulate and react for 25-30 min, and then placing the coagulated reaction mixture into a first-stage defluorination sedimentation tank for natural sedimentation for more than 5.0 h;
and a second-stage defluorination process: conveying the supernatant of the first-stage defluorination sedimentation tank to a second-stage defluorination reaction tank, adding acid hydrochloric acid or sulfuric acid to adjust the pH value to 6.0-7.5, and stirring for 3-5 min; then adding 5 wt% of polymeric ferric sulfate solution, wherein the adding amount is 500 mg/L; PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L; controlling the coagulation and reaction time to be 25-30 min, and then placing the coagulation reaction mixture into a second-stage defluorination sedimentation tank for natural sedimentation for more than 5.0 h; and then, conveying the supernatant in the second sedimentation tank to a double-effect evaporation regulating tank, filtering by a plate-frame type liquid pressing machine, pumping into a double-effect evaporation system, and recovering bromine salt.
Claims (2)
1. A method for recovering bromine salt from a flue gas absorption liquid is characterized in that: the method comprises the steps of mixing a waste circuit board and low-grade impure copper as raw materials, taking limestone, quartz stone and coke as auxiliary materials, absorbing flue gas generated by a pyrogenic process by 30wt% of caustic soda, treating obtained washing liquid by a defluorination pretreatment system, conveying supernate to a double-effect evaporation regulating tank, filtering by a plate-frame type liquid pressing machine, then entering a double-effect evaporation system for evaporation and concentration, and recovering to obtain bromine salt; the defluorination pretreatment system adopts a two-stage defluorination process: the first stage uses Ca (OH)2- CaCl2-combined PAM-PAC defluorination; in the second stage, fluorine is removed by using a polymeric ferric sulfate-PAM-PAC combined method;
the method comprises the following specific steps:
step 1: first stage defluorination
Delivering the washed solution to a first-stage defluorination reaction tank, adding lime emulsion to control the pH to be 10.0, and then adding CaCl2The amount of the added solution is the Ca in the coagulated solution2+The content is 50 mg/L; PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L; controlling the solution to coagulate and react for 25-30 min, and then placing the coagulated reaction mixture into a first-stage defluorination sedimentation tank for natural sedimentation for more than 5.0 h;
step 2: second stage defluorination
Conveying the supernatant in the first-stage defluorination sedimentation tank to a second-stage defluorination reaction tank, adding hydrochloric acid or sulfuric acid to adjust the pH value to 6.0-7.5, and stirring for 3-5 min; then adding 5 wt% of polymeric ferric sulfate solution, wherein the adding amount is 500 mg/L; PAC and PAM medicaments are added simultaneously, wherein the adding amount of the PAC coagulant is 100mg/L, and the adding amount of the PAM flocculating agent is 5.0 mg/L; controlling the coagulation and reaction time to be 25-30 min, and then placing the coagulation reaction mixture into a second-stage defluorination sedimentation tank for natural sedimentation for more than 5.0 h;
and step 3: double effect evaporation concentration
And then, conveying the supernatant in the second sedimentation tank to a double-effect evaporation regulating tank, filtering by a plate-frame type liquid pressing machine, pumping into a double-effect evaporation system for concentration, and recovering to obtain the bromine salt.
2. The method for recovering bromine salt from flue gas absorption liquid according to claim 1, wherein: the steam used by the double-effect evaporation system is sourced from a waste heat boiler.
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| JPH10263558A (en) * | 1997-03-26 | 1998-10-06 | Japan Organo Co Ltd | Treatment of fluorine-containing desulfurized waste water |
| CN1765516A (en) * | 2005-09-13 | 2006-05-03 | 北京化工大学 | A layered material for bromine recovery and method for treating bromine-containing water |
| CN101746874A (en) * | 2010-02-04 | 2010-06-23 | 武汉中新化工有限公司 | Processing method of wastewater desulfurized by fume wet method |
| CN104496063A (en) * | 2014-11-17 | 2015-04-08 | 中国石油集团东北炼化工程有限公司吉林设计院 | Method for removing fluorine in wastewater |
| CN105366839A (en) * | 2015-08-19 | 2016-03-02 | 华电电力科学研究院 | Treatment device and method for simultaneously removing high-concentration SS, fluoride, sulfate, arsenate and COD in desulfurization waste water |
| CN105217869A (en) * | 2015-10-16 | 2016-01-06 | 北京欧泰克能源环保工程技术股份有限公司 | The method of resource of the spent acid produced in a kind of flue gas during smelting Sulphuric acid |
| CN105502782A (en) * | 2015-12-07 | 2016-04-20 | 湖南湘牛环保实业有限公司 | Technology for recovering water resources and salt from coking wastewater in coal chemical industry |
| CN105481179A (en) * | 2015-12-28 | 2016-04-13 | 中国石油集团东北炼化工程有限公司吉林设计院 | Concentrated salt sewage zero-discharge treatment method |
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