CN103159235A - Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace - Google Patents
Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace Download PDFInfo
- Publication number
- CN103159235A CN103159235A CN2013100535435A CN201310053543A CN103159235A CN 103159235 A CN103159235 A CN 103159235A CN 2013100535435 A CN2013100535435 A CN 2013100535435A CN 201310053543 A CN201310053543 A CN 201310053543A CN 103159235 A CN103159235 A CN 103159235A
- Authority
- CN
- China
- Prior art keywords
- solid
- liquid
- solution
- chlorine
- flying dust
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to a method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in a soda recovery furnace. A device for removing the chlorine and potassium ions and recycling the sulfate radicals in the flying ash in the soda recovery furnace is characterized by comprising a dissolving tank, the dissolving tank is connected with an inlet of a third solid-liquid separator, a liquid phase outlet of the third solid-liquid separator is connected with an inlet of a first mixing tank, an outlet of the first mixing tank is connected with an inlet of a first solid-liquid separator, a liquid phase outlet of the first solid-liquid separator is connected with an ion exchange resin device, the ion exchange resin device is connected with an inlet of a second mixing tank, a solid phase outlet of the first solid-liquid separator is connected with a first feeding device, the first feeding device is connected with the inlet of the second mixing tank, an outlet of the second mixing tank is connected with an inlet of a second solid-liquid separator, and a liquid phase outlet of the second solid-liquid separator is connected with a material storing tank. According to the method for removing the chlorine and potassium ions and recycling the sulfate radicals in the flying ash in the soda recovery furnace, removal rate of the chlorine and potassium ions and retention rate of the sulfate radicals are high, and the removal rate and the retention rate are more than 90%.
Description
The application divides an application, and the application number of original application is 201110302443.2, applying date 2011.10.09, name are called " method and apparatus of removing chlorine, potassium ion reclaim(ed) sulfuric acid root in the alkali recovery furnace flying dust "
Technical field
The present invention relates to a kind of method of removing chlorine in the alkali recovery furnace flying dust, potassium ion and reclaim(ed) sulfuric acid root, be used for removing chlorion and the potassium ion of pulp and paper making alkali recovery furnace flying dust, and the reclaim(ed) sulfuric acid radical ion.
Background technology
One of important industry that paper industry develops as Chinese national economy, development in recent years is rapid, and paper and paperboard production rank first in the world.The major way that alkali reclaims as papermaking wastewater processing and energy recovery is widely adopted.As the flying dust of one of the products of combustion of black liquor in alkali recovery furnace, its main component is Na
2SO
4, NaCl, K
2SO
4, KCl, Na
2CO
3And K
2CO
3Deng compound, wherein chlorine and potassium are non-technique element, and the normal operation and the economy that alkali are reclaimed Workshop Production have produced serious harm.As shown in table 1, be the result to domestic two pulp mill's flying dust ultimate analyses, non-technique elemental chlorine, potassium content are higher.In flying dust, the increased content of chlorine and potassium element will increase the tackyness of flying dust, reduce and cohere temperature, and flying dust coheres the reduction of temperature and accelerated the obstruction of alkali recovery furnace flying dust passage.In flying dust, chlorine, too high its main harm of Determination of Potassium have the following aspects: (1) causes the alkali stove fouling and clogging phenomenon frequently to occur, even produces coking when serious, and alkali recovery furnace needs frequent shutdown, cleaning; (2) reduced heat transfer coefficient, vapor temperature, the generated energy of steam turbine decreases, and has increased boiler sootblowing steam consumption; (3) the chlorine element is very harmful in the high temperature corrosion of boi1er tube, and chlorine can corrode the iron and its oxi in carbon steel, and this corrosion is repeated.And Cr and Ni under hot conditions in meeting alloy steel produce corrosion, destroy the fine and close protective membrane on its surface.During greater than 550 ℃, muriatic volatilization is quite violent when temperature, makes corrosion be linear high speed development.Moreover, when having sulfide to coexist, muriatic corrosion is more serious, very easily causes the power parts damages of alkali furnace pressure and causes booster.
Domestic two the pulp mill's flying dust results of elemental analyses of table 1
| ? | K/％ | Na/％ | Si/％ | C/％ | S/％ | Cl -/％ |
| Domestic A factory | 8.2 | 32.8 | 0.026 | 0.043 | 21.0 | 4.3 |
| Domestic B factory | 5.6 | 33.4 | 0.038 | 0.21 | 19.7 | 4.9 |
The method of removing at present chlorine, potassium element in flying dust mainly contains four kinds:
The first: analyse the filter method.Flying dust is dissolved in the hot water of about 90 ℃, and the ratio of controlling flying dust and water makes solution near saturated, because NaCl and KCl compare Na
2SO
4Higher solvability is arranged, work as Na
2SO
4When separating out, the chlorine element still is retained in solution.Adopt solid-liquid separation technique to comprise centrifugation or analyse elimination except chloride NaCl and KCl solution, Na
2SO
4Crystallization is recycled utilization.The advantage of this technology is that technique is simple, and production cost is low; Shortcoming is that clearance and organic efficiency are lower.
The second: evaporation/crystallization method.Adopt the method for selective crystallization to remove chlorine element and potassium element, the filter method is identical with analysing, and this technology is utilized the solubleness of the sodium sulfate principle lower than the solubleness of muriate and sylvite, and adopts evaporation equipment to improve crystallization production efficiency.The shortcoming of this technology is evaporation equipment, complex process, is comprised of three parts as crystal system, is respectively flying dust dissolving unit, selective freezing unit and solids treatment unit, and the facility investment expense is higher.
The third: the crystallisation by cooling method.This technical basis Na
2SO
410H
2The Precipitation Temperature of O has adopted the subcooling crystallization method to isolate Na from NaCl and KCl solution below 20 ℃
2SO
4The advantage of this technology be solid-liquid separation easily and Cl
-Clearance is higher; Shortcoming is cooling the needs to consume a large amount of electric energy, and evaporated water is larger, and production cost is higher.
The 4th kind: ion exchange method.The ion exchange technique principle is different from above three kinds of technology, thereby it is to have strong adsorption to reach the effect of dechlorination by ion exchange resin to chlorion, and this technology is the easiest, but abroad this core technology is maintained secrecy always.
Zirconium hydroxide has different adsorption effects to sulfate ion under condition of different pH, according to this characteristic, zirconium hydroxide is widely used in removing in chlorine industry sulfate ion.Patent of invention ZL94112802.4 discloses the separation method of sulfate ion in a kind of concentrated salt solution, patent of invention CN102086521A discloses a kind of absorption and ceramic membrane coupling technique that removes the sulfate anion in brine system ion, both all only relates to the removal of sulfate anion in brine system ion.The present invention utilizes zirconium hydroxide sulfate radical to be easy to the characteristic of sorption and desorption, and itself and ion exchange resin are combined, and is used for removing sode ash chlorion and potassium ion and keeps to greatest extent sulfate radical.
Summary of the invention
The method that the purpose of this invention is to provide chlorine, potassium ion and reclaim(ed) sulfuric acid root in the removal alkali recovery furnace flying dust that a kind of equipment is simple, cost is low, raw material can reuse.
in order to achieve the above object, the invention provides chlorine in a kind of removal alkali recovery furnace flying dust, the device of potassium ion and reclaim(ed) sulfuric acid root, it is characterized in that, comprise dissolving tank, dissolving tank connects the entrance of the 3rd solid-liquid separator, the liquid-phase outlet of the 3rd solid-liquid separator connects the entrance of the first tempering tank, the outlet of the first tempering tank connects the entrance of the first equipment for separating liquid from solid, the liquid-phase outlet of the first equipment for separating liquid from solid connects Di, Di connects the entrance of the second tempering tank, the solid phase outlet of the first equipment for separating liquid from solid connects the first pay-off, the first pay-off connects the entrance of the second tempering tank, the outlet of the second tempering tank connects the entrance of the second equipment for separating liquid from solid, the liquid-phase outlet of the second equipment for separating liquid from solid connects storagetank.
Preferably, the outlet of the solid phase of described the second equipment for separating liquid from solid connects the second pay-off, and the second pay-off connects the entrance of the first tempering tank.
More preferably, described the first pay-off and the second pay-off are helical screw feeder.
Preferably, the resin in described Di is mixed-bed resin, comprises strong base resin anion(R.A) and sodium type resin cation (R.C.).
Preferably, described the first tempering tank and the second tempering tank are the tempering tank that vertical band stirs.
Preferably, described the 3rd solid-liquid separator is cyclone separator, and described the first equipment for separating liquid from solid and the second equipment for separating liquid from solid are filter or whizzer.
The present invention also provides a kind of method of removing chlorine in the alkali recovery furnace flying dust, potassium ion and reclaim(ed) sulfuric acid root, it is characterized in that, concrete steps are:
The first step: flying dust is added the water stirring and dissolving become saturated solution, will discharge after insolubles separation wherein;
Second step: the pH value of the first step gained solution is adjusted to 2～4, and (structural formula is ZrO (OH) to add zirconium hydroxide
2), stirring makes solution fully contact with zirconium hydroxide, with the sulfate radical (SO in adsorbent solution
4 2-);
The 3rd step: the solution of second step gained is carried out solid-liquid separation obtain liquid phase and solid phase, the liquid phase spent ion exchange resin of gained is carried out ion-exchange remove the solution that obtains containing sodium hydroxide after chlorion and potassium ion, with the solid phase mixing of gained;
The 4th step: the pH value of mixed solution of the 3rd step gained is adjusted to 12～14, fully stirs, make sulfate ion that zirconium hydroxide adsorbs parse and obtain suspension liquid;
The 5th step: with the suspension liquid solid-liquid separation of the 4th step gained, liquid phase is mixed with rare black liquor carry out evaporation and concentrating.
Preferably, in described second step in zirconium hydroxide and sode ash the mol ratio of sulfate radical be 2～6: 1.
Preferably, the solid phase of the solid-liquid separation gained in described the 5th step is zirconium hydroxide, and described solid phase is reclaimed, and is used for second step as the zirconium hydroxide raw material and adsorbs sulfate radical.
Compared with prior art, the present invention has following advantage:
(1) sode ash is dissolved into saturated solution, has reduced to greatest extent the consumption of water, is also that follow-up evaporation process reduces energy consumption.
(2) chlorine, potassium ion clearance and sulfate ion retention rate are all very high, reach more than 90%.
(3) adopt and be conventional equipment, with low cost; Whole dechlorination, potassium process need not heating or cooling, and energy consumption is low.
(4) raw material can reuse, and reduces raw materials cost.The main raw material zirconium hydroxide need not subsequent disposal after solid-liquid separation for the second time, can direct reuse, and mixed-bed resin is also reusable after desorption.Waste liquid after zirconium hydroxide absorption after sulfate ion is processed by Di chlorine, the potassium element removed wherein again and is obtained NaOH solution, can be directly used in zirconium hydroxide and resolve the sulfate ion stage, and the water in system and Na element are fully utilized.
(5) the whole process waste discharge is few: except the insolubles that cyclone separator is removed almost without any waste discharge.
Description of drawings
Fig. 1 is for removing the device schematic diagram of chlorine, potassium ion and reclaim(ed) sulfuric acid root in the alkali recovery furnace flying dust.
Embodiment
The invention will be further described below by embodiment.
Embodiment 1
as shown in Figure 1, for removing chlorine in the alkali recovery furnace flying dust, the apparatus structure schematic diagram of potassium ion and reclaim(ed) sulfuric acid root, chlorine in described removal alkali recovery furnace flying dust, the device of potassium ion and reclaim(ed) sulfuric acid root comprises dissolving tank 1, dissolving tank 1 connects the entrance of the 3rd solid-liquid separator 2, the liquid-phase outlet of the 3rd solid-liquid separator 2 connects the entrance of the first tempering tank 3, the outlet of the first tempering tank 3 connects the entrance of the first equipment for separating liquid from solid 4, the liquid-phase outlet of the first equipment for separating liquid from solid 4 connects Di 5, Di 5 connects the entrance of the second tempering tank 7, the solid phase outlet of the first equipment for separating liquid from solid 4 connects the first pay-off 6, the first pay-off 6 connects the entrance of the second tempering tank 7, the outlet of the second tempering tank 7 connects the entrance of the second equipment for separating liquid from solid 8, the liquid-phase outlet of the second equipment for separating liquid from solid 8 connects storagetank 9.The solid phase outlet of described the second equipment for separating liquid from solid 8 connects the entrance that the second pay-off 10, the second pay-offs 10 connect the first tempering tank 3.Described the first pay-off 6 and the second pay-off 10 are helical screw feeder.Resin in described Di 5 is mixed-bed resin, comprises strong base resin anion(R.A) and sodium type resin cation (R.C.).Described the first tempering tank 3 and the second tempering tank 7 are the tempering tank that vertical band stirs.Described the 3rd solid-liquid separator 2 is cyclone separator, and described the first equipment for separating liquid from solid 4 and the second equipment for separating liquid from solid 8 are whizzer.
Adopt the device of chlorine, potassium ion and reclaim(ed) sulfuric acid root in above-mentioned removal alkali recovery furnace flying dust to remove the method for chlorine, potassium ion reclaim(ed) sulfuric acid root in the alkali recovery furnace flying dust as follows:
The first step: flying dust is collected dissolving tank 1 add the water stirring and dissolving and become saturated solution, mixed solution is passed into the 3rd solid-liquid separator 2, remove insolubles;
Second step: the sode ash solution after the removal of impurity is passed into the first tempering tank 3, and toward wherein adding a certain amount of hydrochloric acid, regulate pH to 2, add zirconium hydroxide by 2 times of sulfate radical content mole number in sode ash, stirring makes solution fully contact with zirconium hydroxide, the sulfate radical SO in adsorbent solution
4 2-
The 3rd step: the suspension liquid in the first tempering tank 3 is transported to the first equipment for separating liquid from solid 4 carries out solid-liquid separation, solid phase is transported to the second tempering tank 7 by the first pay-off 6, liquid phase is transported to Di 5, liquid phase and strongly basic anionic resin and sodium type resin cation (R.C.) carry out ion-exchange, remove the solution that chlorion and potassium ion obtain containing NaOH, this part solution also is transported to the second tempering tank 7;
The 4th step: add NaOH solution to regulate pH value 12 in the second tempering tank 7, fully stir, the sulfate ion that zirconium hydroxide is adsorbed parses;
The 5th step: the suspension liquid in the second tempering tank 7 is transported to the second equipment for separating liquid from solid 8 carries out solid-liquid separation, liquid phase is for containing Na
2SO
4Solution, be transported to storagetank 9 and be used for the black liquor vaporizing section, mix with rare black liquor and carry out evaporation and concentrating, solid phase is zirconium hydroxide, is transported to the first tempering tank 3 reuses by the second pay-off 10.
Embodiment 2
as shown in Figure 1, for removing chlorine in the alkali recovery furnace flying dust, the apparatus structure schematic diagram of potassium ion and reclaim(ed) sulfuric acid root, chlorine in described removal alkali recovery furnace flying dust, the device of potassium ion and reclaim(ed) sulfuric acid root comprises dissolving tank 1, dissolving tank 1 connects the entrance of the 3rd solid-liquid separator 2, the liquid-phase outlet of the 3rd solid-liquid separator 2 connects the entrance of the first tempering tank 3, the outlet of the first tempering tank 3 connects the entrance of the first equipment for separating liquid from solid 4, the liquid-phase outlet of the first equipment for separating liquid from solid 4 connects Di 5, Di 5 connects the entrance of the second tempering tank 7, the solid phase outlet of the first equipment for separating liquid from solid 4 connects the first pay-off 6, the first pay-off 6 connects the entrance of the second tempering tank 7, the outlet of the second tempering tank 7 connects the entrance of the second equipment for separating liquid from solid 8, the liquid-phase outlet of the second equipment for separating liquid from solid 8 connects storagetank 9.The solid phase outlet of described the second equipment for separating liquid from solid 8 connects the entrance that the second pay-off 10, the second pay-offs 10 connect the first tempering tank 3.Described the first pay-off 6 and the second pay-off 10 are helical screw feeder.Resin in described Di 5 is mixed-bed resin, comprises strong base resin anion(R.A) and sodium type resin cation (R.C.).Described the first tempering tank 3 and the second tempering tank 7 are the tempering tank that vertical band stirs.Described the 3rd solid-liquid separator 2 is cyclone separator, and described the first equipment for separating liquid from solid 4 and the second equipment for separating liquid from solid 8 are whizzer.
Adopt the device of chlorine, potassium ion and reclaim(ed) sulfuric acid root in above-mentioned removal alkali recovery furnace flying dust to remove the method for chlorine, potassium ion reclaim(ed) sulfuric acid root in the alkali recovery furnace flying dust as follows:
The first step: flying dust is collected dissolving tank 1 add the water stirring and dissolving and become saturated solution, mixed solution is passed into the 3rd solid-liquid separator 2, remove insolubles;
Second step: the sode ash solution after the removal of impurity is passed into the first tempering tank 3, and toward wherein adding a certain amount of sulfuric acid, regulate pH to 3, add zirconium hydroxide by 6 times of sulfate radical content mole number in sode ash, stirring makes solution fully contact with zirconium hydroxide, the sulfate radical SO in adsorbent solution
4 2-
The 3rd step: the suspension liquid in the first tempering tank 3 is transported to the first equipment for separating liquid from solid 4 carries out solid-liquid separation, solid phase is transported to the second tempering tank 7 by the first pay-off 6, liquid phase is transported to Di 5, liquid phase and strongly basic anionic resin and sodium type resin cation (R.C.) carry out ion-exchange, remove the solution that chlorion and potassium ion obtain containing NaOH, this part solution also is transported to the second tempering tank 7;
The 4th step: add NaOH solution to regulate pH value 13 in the second tempering tank 7, fully stir, the sulfate ion that zirconium hydroxide is adsorbed parses;
The 5th step: the suspension liquid in the second tempering tank 7 is transported to the second equipment for separating liquid from solid 8 carries out solid-liquid separation, liquid phase is for containing Na
2SO
4Solution, be transported to storagetank 9 and be used for the black liquor vaporizing section, mix with rare black liquor and carry out evaporation and concentrating, solid phase is zirconium hydroxide, is transported to the first tempering tank 3 reuses by the second pay-off 10.
Embodiment 3
as shown in Figure 1, for removing chlorine in the alkali recovery furnace flying dust, the apparatus structure schematic diagram of potassium ion and reclaim(ed) sulfuric acid root, chlorine in described removal alkali recovery furnace flying dust, the device of potassium ion and reclaim(ed) sulfuric acid root comprises dissolving tank 1, dissolving tank 1 connects the entrance of the 3rd solid-liquid separator 2, the liquid-phase outlet of the 3rd solid-liquid separator 2 connects the entrance of the first tempering tank 3, the outlet of the first tempering tank 3 connects the entrance of the first equipment for separating liquid from solid 4, the liquid-phase outlet of the first equipment for separating liquid from solid 4 connects Di 5, Di 5 connects the entrance of the second tempering tank 7, the solid phase outlet of the first equipment for separating liquid from solid 4 connects the first pay-off 6, the first pay-off 6 connects the entrance of the second tempering tank 7, the outlet of the second tempering tank 7 connects the entrance of the second equipment for separating liquid from solid 8, the liquid-phase outlet of the second equipment for separating liquid from solid 8 connects storagetank 9.The solid phase outlet of described the second equipment for separating liquid from solid 8 connects the entrance that the second pay-off 10, the second pay-offs 10 connect the first tempering tank 3.Described the first pay-off 6 and the second pay-off 10 are helical screw feeder.Resin in described Di 5 is mixed-bed resin, comprises strong base resin anion(R.A) and sodium type resin cation (R.C.), and resin is renewable.Described the first tempering tank 3 and the second tempering tank 7 are the tempering tank that vertical band stirs.Described the 3rd solid-liquid separator 2 is cyclone separator, and described the first equipment for separating liquid from solid 4 and the second equipment for separating liquid from solid 8 are whizzer.
Adopt the device of chlorine, potassium ion and reclaim(ed) sulfuric acid root in above-mentioned removal alkali recovery furnace flying dust to remove the method for chlorine, potassium ion reclaim(ed) sulfuric acid root in the alkali recovery furnace flying dust as follows:
The first step: flying dust is collected dissolving tank 1 add the water stirring and dissolving and become saturated solution, mixed solution is passed into the 3rd solid-liquid separator 2, remove insolubles;
Second step: the sode ash solution after the removal of impurity is passed into the first tempering tank 3, and toward wherein adding a certain amount of nitric acid, regulate pH to 4, add zirconium hydroxide by 4 times of sulfate radical content mole number in sode ash, stirring makes solution fully contact with zirconium hydroxide, the sulfate radical SO in adsorbent solution
4 2-
The 3rd step: the suspension liquid in the first tempering tank 3 is transported to the first equipment for separating liquid from solid 4 carries out solid-liquid separation, solid phase is transported to the second tempering tank 7 by the first pay-off 6, liquid phase is transported to Di 5, liquid phase and strongly basic anionic resin and sodium type resin cation (R.C.) carry out ion-exchange, remove the solution that chlorion and potassium ion obtain containing NaOH, this part solution also is transported to the second tempering tank 7;
The 4th step: add NaOH solution to regulate pH value 14 in the second tempering tank 7, fully stir, the sulfate ion that zirconium hydroxide is adsorbed parses;
The 5th step: the suspension liquid in the second tempering tank 7 is transported to the second equipment for separating liquid from solid 8 carries out solid-liquid separation, liquid phase is for containing Na
2SO
4Solution, be transported to storagetank 9 and be used for the black liquor vaporizing section, mix with rare black liquor and carry out evaporation and concentrating, solid phase is zirconium hydroxide, is transported to the first tempering tank 3 reuses by the second pay-off 10.
Each case process condition and operation result see the following form 2:
Each example operation result of table 2:
In embodiment, the definition of chlorion clearance, potassium ion clearance and sulfate radical retention rate is respectively:
Claims (3)
1. a method of removing chlorine in the alkali recovery furnace flying dust, potassium ion and reclaim(ed) sulfuric acid root, is characterized in that, concrete steps are:
The first step: flying dust is added the water stirring and dissolving become saturated solution, will discharge after insolubles separation wherein;
Second step: the pH value of the first step gained solution is adjusted to 2～4, adds zirconium hydroxide, stirring makes solution fully contact with zirconium hydroxide, with the sulfate radical in adsorbent solution;
The 3rd step: the solution of second step gained is carried out solid-liquid separation obtain liquid phase and solid phase, the liquid phase spent ion exchange resin of gained is carried out ion-exchange remove the solution that obtains containing sodium hydroxide after chlorion and potassium ion, with the solid phase mixing of gained;
The 4th step: the pH value of mixed solution of the 3rd step gained is adjusted to 12～14, fully stirs, make sulfate ion that zirconium hydroxide adsorbs parse and obtain suspension liquid;
The 5th step: with the suspension liquid solid-liquid separation of the 4th step gained, liquid phase is mixed with rare black liquor carry out evaporation and concentrating.
2. the method for chlorine, potassium ion and reclaim(ed) sulfuric acid root in removal alkali recovery furnace flying dust as claimed in claim 1, is characterized in that, in described second step in zirconium hydroxide and alkali recovery furnace flying dust the mol ratio of sulfate radical be 2～6: 1.
3. the method for chlorine, potassium ion and reclaim(ed) sulfuric acid root in removal alkali recovery furnace flying dust as claimed in claim 1, it is characterized in that, the solid phase of the solid-liquid separation gained in described the 5th step is zirconium hydroxide, the solid phase of the solid-liquid separation gained in described the 5th step is reclaimed, be used for second step as the zirconium hydroxide raw material and adsorb sulfate radical.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310053543.5A CN103159235B (en) | 2011-10-09 | 2011-10-09 | Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310053543.5A CN103159235B (en) | 2011-10-09 | 2011-10-09 | Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110302443 Division CN102432038B (en) | 2011-10-09 | 2011-10-09 | Method and device for removing chlorine and potassium ions in fly ash produced by alkali recovery furnace and recovering sulfate radical |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103159235A true CN103159235A (en) | 2013-06-19 |
| CN103159235B CN103159235B (en) | 2014-09-24 |
Family
ID=48582816
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310053543.5A Active CN103159235B (en) | 2011-10-09 | 2011-10-09 | Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103159235B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5071563A (en) * | 1989-11-09 | 1991-12-10 | Kanegafuchi Kagaku Kogyo Kabushiki Kaisha | Method for removing sulfate ions from aqueous solution of alkali metal chloride |
| CN1107804A (en) * | 1993-10-06 | 1995-09-06 | 埃勒夫阿托化学有限公司 | Process for the removal of sulphate ions present in saline solutions |
| CA2219550A1 (en) * | 1996-11-01 | 1998-05-01 | Sterling Canada, Inc. | A method of recovery of chemical compounds from a pulp mill |
| CN102086521A (en) * | 2010-12-10 | 2011-06-08 | 江苏久吾高科技股份有限公司 | Adsorption and ceramic membrane coupling process for removing sulfate ions from saline water |
-
2011
- 2011-10-09 CN CN201310053543.5A patent/CN103159235B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5071563A (en) * | 1989-11-09 | 1991-12-10 | Kanegafuchi Kagaku Kogyo Kabushiki Kaisha | Method for removing sulfate ions from aqueous solution of alkali metal chloride |
| CN1107804A (en) * | 1993-10-06 | 1995-09-06 | 埃勒夫阿托化学有限公司 | Process for the removal of sulphate ions present in saline solutions |
| CA2219550A1 (en) * | 1996-11-01 | 1998-05-01 | Sterling Canada, Inc. | A method of recovery of chemical compounds from a pulp mill |
| CN102086521A (en) * | 2010-12-10 | 2011-06-08 | 江苏久吾高科技股份有限公司 | Adsorption and ceramic membrane coupling process for removing sulfate ions from saline water |
Non-Patent Citations (1)
| Title |
|---|
| LICI´NIO MANUEL G. A. FERREIRA: "Removal of Chloride in the Kraft Chemical Recovery Cycle of Pulp Mills Using the Ion-Exchange Process", 《IND. ENG. CHEM. RES.》 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103159235B (en) | 2014-09-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102145905B (en) | Method for preparing metallurgy-level aluminum oxide by using fluidized bed pulverized fuel ash | |
| CN110217810B (en) | Method for efficiently recovering valuable elements in aluminum ash | |
| CN108217700B (en) | System and method for preparing battery-grade lithium carbonate | |
| CN101161596A (en) | A method for resource processing non-ferro metals processing wastewater containing ammonia and sulfate radical | |
| CN109095578B (en) | Method for recovering calcium and magnesium in power plant desulfurization wastewater by oxalic acid precipitation method | |
| CN110655258A (en) | Novel integrated treatment system and process for zero discharge of high-salinity wastewater in coal chemical industry | |
| CN103950991A (en) | Waste acid and wastewater treatment process in processes of pickling and purifying quartz or feldspar | |
| CN112941328A (en) | Treatment method for recycling fly ash | |
| CN108218096B (en) | System and method for treating mercury-containing high-salt wastewater from chloroethylene production by calcium carbide method | |
| CN103318918B (en) | A kind of method of purifying and recovering ammonia gas | |
| CN104649335A (en) | Method and device for recycling ferrous chloride crystal and hydrochloric acid from chlorohydric acid pickling waste solution | |
| CN103482655B (en) | Lime-sodium sulfate-carbon dioxide method used for purifying calcium chloride type bittern | |
| CN102587187B (en) | Alkali recovery method for by-producing activated carbon and white carbon black by using paper making black liquid | |
| CN102432038B (en) | Method and device for removing chlorine and potassium ions in fly ash produced by alkali recovery furnace and recovering sulfate radical | |
| CN103818969A (en) | Iron oxide red and preparation method thereof | |
| CN110817907B (en) | Treatment system and method for purifying high-purity lithium carbonate | |
| CN101209844B (en) | Technique for preparing high quality boric acid from salt lake type boron ore by one-step method | |
| CN109133125A (en) | A method of Magnesium Hydroxide Nano-particles are prepared using wet desulphurization waste water | |
| CN103159235B (en) | Method for removing chlorine and potassium ions and recycling sulfate radicals in flying ash in soda recovery furnace | |
| CN108658353B (en) | Calcium chloride wastewater treatment process | |
| CN102247742A (en) | Purification process for sintering flue gas desulfurization solution | |
| TWM632048U (en) | Resource recovery system for waste liquid boron | |
| CN112723513B (en) | Treatment process for purifying chlorine-containing wastewater by ammonium salt crystallization | |
| CN107459054A (en) | A kind of desulfurization wastewater technique of zero discharge using carbon dioxide process | |
| CN109536708B (en) | Method for separating chromium and iron in pickling waste liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |