CN102730722B - Method for preparing refined strong brine by removing potassium from strong brine - Google Patents
Method for preparing refined strong brine by removing potassium from strong brine Download PDFInfo
- Publication number
- CN102730722B CN102730722B CN 201210245534 CN201210245534A CN102730722B CN 102730722 B CN102730722 B CN 102730722B CN 201210245534 CN201210245534 CN 201210245534 CN 201210245534 A CN201210245534 A CN 201210245534A CN 102730722 B CN102730722 B CN 102730722B
- Authority
- CN
- China
- Prior art keywords
- strong brine
- potassium
- ion exchange
- exchange column
- raw material
- 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.)
- Active
Links
Abstract
The invention provides a method for preparing refined strong brine by removing potassium from strong brine, and relates to a method for removing potassium from strong brine. The method comprises the following steps of: under the temperature of 15-40DEG C, introducing raw material strong brine into an ion exchange column filled with modified zeolite to carry out an adsorbing reaction, adsorbing the raw material strong brine by an analogue moving bed technology till exchange reaction between the potassium ions in the raw material strong brine and the sodium ions on the modified zeolite is completed, and adsorbing to obtain the refined strong brine of which the K<+> content is 0.10g/L-0.39g/L; and eluting potassium ions in the ion exchange column after adsorption in the first step by taking saturated sodium chloride solution as eluant under the temperature of 25-95DEG C, so that the potassium-rich solution of which the potassium ion concentration is 10.23g/L-12.67g/L can be obtained, and the ion exchange column can be recycled after being eluted by the saturated sodium chloride solution. According to the method provided by the invention, the potassium ions in the electrically-dialysed strong brine can be effectively removed, and the qualified brine which meets the requirement of the chlor-alkali industry can be prepared.
Description
Technical field
Technical scheme of the present invention relates to removes potassium, the method for specifically from strong brine, except the potassium preparation, making with extra care strong brine from salt solution.
Background technology
Refining strong brine mainly contains two large purposes, and the one, for salt manufacturing, the 2nd, for chlor-alkali industry.Because the main source of salt is seawater, follow the aggravation of coastland land used pressure, batch production salt manufacturing will finally replace tradition and evaporate brine, particularly follow the development of extensive sea water desaltination industry, take seawater or concentrated seawater as raw material, and the batch production salt manufacturing pattern that the electrodialysis of take liquid salt processed is representative will be adopted gradually.The strong brine obtained after electrodialysis generally contains a small amount of K
+, Ca
2+, Mg
2+and SO
4 2-, Ca in salt solution
2+, Mg
2+and SO
4 2-removal come into one's own always, the removal method is comparatively ripe.For example, CN1107121A discloses a kind of " utilizing the method for the standby refined brine of making from brine ", is mainly to utilize precipitin reaction to remove the Ca in bittern and salt solution
2+, Mg
2+, SO
4 2-; CN1019095B discloses " a kind of method that purifies sodium chloride brine and bittern ", is mainly the SO removed in salt solution and bittern
4 2-and Ca
2+; CN1147429C discloses a kind of method of refined brine, is mainly the calcium magnesium of removing in salt solution.In the process for refining of the strong brine obtained after existing electroosmose process, to K
+removal also there is no what effective means, and K
+existence directly affect the purity of quality, the especially caustic soda of chlor-alkali industry product.Therefore, the strong brine obtained after refining electrodialysis, particularly remove K wherein
+, to make the qualified salt solution that meets the chlor-alkali industry requirement, be the chlor-alkali industry active demand.At present, there is not yet in the relevant strong brine obtained from electroosmose process and remove K
+make the bibliographical information of refining strong brine.
Summary of the invention
Technical problem to be solved by this invention is: the method for from strong brine, except the potassium preparation, making with extra care strong brine is provided, it is a kind of method of with modified zeolite, except the potassium preparation, making with extra care strong brine, can effectively remove the potassium ion in the strong brine obtained after electrodialysis, to make the qualified salt solution that meets the chlor-alkali industry requirement.
The present invention solves this technical problem adopted technical scheme: from strong brine, except the method for the refining strong brine of potassium preparation, be a kind of method of removing the refining strong brine of potassium preparation with modified zeolite, concrete steps are:
The first step, carry out the absorption of raw material strong brine except potassium with the ion exchange column of filling modified zeolite, makes refining strong brine
Under 15～40 ℃, the raw material strong brine is passed in the ion exchange column that loads modified zeolite and carries out absorption reaction, the potassium ion and the sodium ion generation permutoid reaction on modified zeolite that the raw material strong brine are adsorbed in the raw material strong brine with simulated moving bed technology are complete, obtain K after suction
+the refining strong brine that content is 0.10g/L～0.39g/L;
Second step, carry out wash-out to the potassium ion in the ion exchange column after inhaling
At 25 ℃～95 ℃ temperature with saturated nacl aqueous solution as eluent to the first step in absorption after ion exchange column in potassium ion carry out wash-out, obtain containing the rich potassium solution that potassium concentration is 10.23g/L～12.67g/L, this ion exchange column is through recycle after the wash-out of saturated nacl aqueous solution.
Above-mentioned method of from strong brine, except the potassium preparation, making with extra care strong brine, described raw material strong brine is the strong brine obtained after electrodialysis.
Above-mentioned method of from strong brine, except the potassium preparation, making with extra care strong brine, the ion exchange column of described filling modified zeolite is divided into by single the ion exchange column of 6～12 that 2～4 operating units form, every single ion exchange column is by being 36mm at diameter and being highly to load modified zeolite 800g in the cylinder of 1000mm to form, and 3 ion exchange columns are set as an operating unit.
Above-mentioned method of from strong brine, except the potassium preparation, making with extra care strong brine, the concrete technology of described simulated moving bed technology is, the packed height of controlling in ion exchange column is 6m～12m, every 3m is an operating unit, each operating unit passes into strong brine 3L～21L, and the absorption flow velocity of raw material strong brine is that the void tower flow rate control is at 7m/h～12m/h.
Above-mentioned method of from strong brine, except the potassium preparation, making with extra care strong brine, the strong brine obtained after raw material electrodialysis used, modified zeolite, ion exchange column cylinder and saturated nacl aqueous solution all easily obtain by known approach, and described technique is that those skilled in the art is known.
The invention has the beneficial effects as follows: compared with prior art, the marked improvement that the present invention removes the method for the refining strong brine of potassium preparation from strong brine is:
(1) effectively remove the potassium in the strong brine obtained after electrodialysis, K in the refining strong brine obtained after suction
+content is 0.10g/L～0.39g/L, must make with extra care strong brine after suction and can be used for chlor-alkali industry, and being applied to the caustic soda industry can effectively improve the quality of products, and makes high-purity caustic soda.
(2), simultaneously for chlor-alkali industry provides Yan Heshui, save its traditional change salt operation and reach the demand to fresh water.
(3) adopt simulated moving bed technology, K in the refining strong brine obtained after making to inhale
+content is low and stable, and in salt solution, the potassium ion decreasing ratio can reach more than 95%; The rich potassium solution composition obtained is uniform and stable
(4) the inventive method raw material is easy to get, technique is simple, low cost and efficient.
Embodiment
Embodiment 1
The first step, carry out the absorption of raw material strong brine except potassium with the ion exchange column of filling modified zeolite
Under 25 ℃, the strong brine obtained after the raw material electrodialysis is passed in the ion exchange column that loads modified zeolite and carries out absorption reaction, the ion exchange column of this filling modified zeolite is to be divided into 3 operating units by single the ion exchange column of 9 to form, every single ion exchange column is by being 36mm at diameter and being highly to load modified zeolite 800g in the cylinder of 1000mm to form, and 3 ion exchange columns are set as an operating unit.The potassium ion and the sodium ion generation permutoid reaction on modified zeolite that the raw material strong brine are adsorbed in the raw material strong brine with simulated moving bed technology are complete, concrete technology is: the packed height of controlling in ion exchange column is 9m, every 3m is an operating unit, each operating unit passes into strong brine 3L, the absorption flow velocity of raw material strong brine be the void tower flow rate control at 7m/h, obtain K after suction
+the refining strong brine that content is 0.39g/L, before and after modified zeolite absorption, the composition of strong brine is in Table 1;
Second step, carry out wash-out to the potassium ion in the ion exchange column after inhaling
At 95 ℃ of temperature with saturated nacl aqueous solution as eluent to the first step in absorption after ion exchange column in potassium ion carry out wash-out, obtain the rich potassium solution that 1.8L is 12.67g/L containing potassium concentration, be recycled after the wash-out of this ion exchange column through saturated nacl aqueous solution.The composition of the rich potassium solution obtained after taking off thus is in Table 2.
Adsorb the composition of front and back strong brine in table 1. embodiment 1 through modified zeolite
In table 2. embodiment 1 with the composition of the rich potassium solution obtained after the saturated nacl aqueous solution wash-out
Embodiment 2
The first step, carry out the absorption of raw material strong brine except potassium with the ion exchange column of filling modified zeolite
Under 15 ℃, the raw material strong brine is passed in the ion exchange column that loads modified zeolite and carries out absorption reaction, the ion exchange column of this filling modified zeolite is divided into by single the ion exchange column of 12 that 4 operating units form, every single ion exchange column is by being 36mm at diameter and being highly to load modified zeolite 800g in the cylinder of 1000mm to form, and 3 ion exchange columns are set as an operating unit.The potassium ion and the sodium ion generation permutoid reaction on modified zeolite that the raw material strong brine are adsorbed in the raw material strong brine with simulated moving bed technology are complete, concrete technology is: the packed height of controlling in ion exchange column is 12m, every 3m is an operating unit, each operating unit passes into strong brine 8L, the absorption flow velocity of raw material strong brine be the void tower flow rate control at 10m/h, obtain K after suction
+the refining strong brine that content is 0.13g/L, before and after modified zeolite absorption, the composition of strong brine is in Table 3;
Second step, carry out wash-out to the potassium ion in the ion exchange column after inhaling
At 60 ℃ of temperature with saturated nacl aqueous solution as eluent to the first step in absorption after ion exchange column in potassium ion carry out wash-out, obtain the rich potassium solution that 2.5L is 11.45g/L containing potassium concentration, be recycled after the wash-out of this ion exchange column through saturated nacl aqueous solution.The composition of the rich potassium solution obtained after taking off thus is in Table 4.
Adsorb the composition of front and back strong brine in table 3. embodiment 2 through modified zeolite
In table 4. embodiment 2 with the composition of the rich potassium solution obtained after the saturated nacl aqueous solution wash-out
Embodiment 3
The first step, carry out the absorption of raw material strong brine except potassium with the ion exchange column of filling modified zeolite
Under 40 ℃, the raw material strong brine is passed in the ion exchange column that loads modified zeolite and carries out absorption reaction, the ion exchange column of this filling modified zeolite is divided into by single the ion exchange column of 6 that 2 operating units form, every single ion exchange column is by being 36mm at diameter and being highly to load modified zeolite 800g in the cylinder of 1000mm to form, and 3 ion exchange columns are set as an operating unit.The potassium ion and the sodium ion generation permutoid reaction on modified zeolite that the raw material strong brine are adsorbed in the raw material strong brine with simulated moving bed technology are complete, concrete technology is: the packed height of controlling in ion exchange column is 6m, every 3m is an operating unit, each operating unit passes into strong brine 21L, the absorption flow velocity of raw material strong brine be the void tower flow rate control at 12m/h, obtain K after suction
+the refining strong brine that content is 0.10g/L, before and after modified zeolite absorption, the composition of strong brine is in Table 5;
Second step, carry out wash-out to the potassium ion in the ion exchange column after inhaling
Under 25 ℃ of degree with saturated nacl aqueous solution as eluent to the first step in absorption after ion exchange column in potassium ion carry out wash-out, obtain containing the rich potassium solution that potassium concentration is 10.23g/L, be recycled after the wash-out of this ion exchange column through saturated nacl aqueous solution.The composition of the rich potassium solution obtained after taking off thus is in Table 6.
Adsorb the composition of front and back strong brine in table 5. embodiment 3 through modified zeolite
In table 6. embodiment 3 with the composition of the rich potassium solution obtained after the saturated nacl aqueous solution wash-out
In above-described embodiment, the strong brine obtained after raw material electrodialysis used, modified zeolite, ion exchange column cylinder and saturated nacl aqueous solution all easily obtain by known approach, and described technique is that those skilled in the art is known.
Claims (1)
1. the method made from extra care strong brine except the potassium preparation from strong brine is characterized in that: be a kind of method of removing the refining strong brine of potassium preparation with modified zeolite, concrete steps are:
The first step, carry out the absorption of raw material strong brine except potassium with the ion exchange column of filling modified zeolite, makes refining strong brine
Under 15～40 ℃, the raw material strong brine is passed in the ion exchange column that loads modified zeolite and carries out absorption reaction, the potassium ion and the sodium ion generation permutoid reaction on modified zeolite that the raw material strong brine are adsorbed in the raw material strong brine with simulated moving bed technology are complete, obtain K after suction
+the refining strong brine that content is 0.10g/L～0.39g/L, the ion exchange column of described filling modified zeolite is divided into by single the ion exchange column of 6～12 that 2～4 operating units form, every single ion exchange column is by being 36 mm at diameter and being highly to load modified zeolite 800g in the cylinder of 1000 mm to form, 3 ion exchange columns are set as an operating unit, the concrete technology of described simulated moving bed technology is, the packed height of controlling in ion exchange column is 6m～12m, every 3m is an operating unit, each operating unit passes into strong brine 3L～21L, the absorption flow velocity of raw material strong brine is that the void tower flow rate control is at 7m/h～12m/h,
Second step, carry out wash-out to the potassium ion in the ion exchange column after inhaling
At 25 ℃～95 ℃ temperature with saturated nacl aqueous solution as eluent to the first step in absorption after ion exchange column in potassium ion carry out wash-out, obtain containing the rich potassium solution that potassium concentration is 10.23g/L～12.67g/L, this ion exchange column is through recycle after the wash-out of saturated nacl aqueous solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201210245534 CN102730722B (en) | 2012-07-17 | 2012-07-17 | Method for preparing refined strong brine by removing potassium from strong brine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201210245534 CN102730722B (en) | 2012-07-17 | 2012-07-17 | Method for preparing refined strong brine by removing potassium from strong brine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102730722A CN102730722A (en) | 2012-10-17 |
| CN102730722B true CN102730722B (en) | 2013-11-06 |
Family
ID=46987128
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201210245534 Active CN102730722B (en) | 2012-07-17 | 2012-07-17 | Method for preparing refined strong brine by removing potassium from strong brine |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102730722B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107285430A (en) * | 2016-04-05 | 2017-10-24 | 亚太森博（山东）浆纸有限公司 | A kind of salt dissolving pond, chlor-alkali salt water treating system and chlor-alkali saline treatment technique |
| CN108996521B (en) * | 2018-08-07 | 2021-03-26 | 泉州师范学院 | Process for producing high-purity refined salt by using selective electrodialysis concentrated brine |
| CN112723388A (en) * | 2020-12-25 | 2021-04-30 | 卢广荣 | Preparation method of medical potassium-free micro-sodium salt |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6066257A (en) * | 1998-08-04 | 2000-05-23 | Calgon Carbon Corporation | Process for the removal and destruction of perchlorate and nitrate from aqueous streams |
| CN1747771A (en) * | 2003-02-04 | 2006-03-15 | 独立行政法人产业技术总合研究所 | Method of reducing impurity content in aqueous salt solution |
| CN100999364A (en) * | 2006-05-16 | 2007-07-18 | 葛文宇 | Comprehensive utilization high advantage zero discharge seawater desalination production technology |
| CN101850991A (en) * | 2010-01-14 | 2010-10-06 | 河北工业大学 | Method for preparing potassium chloride from seawater |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005009578A2 (en) * | 2003-07-16 | 2005-02-03 | Amalgamated Research, Inc. | Method for the recovery of acids from hydrometallurgy process solutions |
-
2012
- 2012-07-17 CN CN 201210245534 patent/CN102730722B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6066257A (en) * | 1998-08-04 | 2000-05-23 | Calgon Carbon Corporation | Process for the removal and destruction of perchlorate and nitrate from aqueous streams |
| CN1747771A (en) * | 2003-02-04 | 2006-03-15 | 独立行政法人产业技术总合研究所 | Method of reducing impurity content in aqueous salt solution |
| CN100999364A (en) * | 2006-05-16 | 2007-07-18 | 葛文宇 | Comprehensive utilization high advantage zero discharge seawater desalination production technology |
| CN101850991A (en) * | 2010-01-14 | 2010-10-06 | 河北工业大学 | Method for preparing potassium chloride from seawater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102730722A (en) | 2012-10-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102730722B (en) | Method for preparing refined strong brine by removing potassium from strong brine | |
| CN108660476B (en) | A kind of new process of salt lake bittern production high-purity hydrogen lithia | |
| CN104803399B (en) | Method for preparing high-purity magnesium oxalate, lithium carbonate and high-purity nanometer magnesia from salt lake brine of high magnesium-lithium ratio | |
| CN104291523A (en) | Method for recovering sodium chloride and glycerin from glycerin-containing high-salinity organic wastewater | |
| CN102730721B (en) | Recovering method of by-product sodium chloride in polyphenylene sulfide production | |
| CN108385128A (en) | A kind of new process of salt lake bittern production high-purity hydrogen lithia | |
| EP2041029B1 (en) | Process for the production of sodium carbonate and sodium bicarbonate | |
| CN104402855B (en) | A kind of dehydration rectification technique of vinylene carbonate | |
| AU2012222624A8 (en) | Treatment of raw brines from desalination plants | |
| CN102774929B (en) | Method for recovering phosphor from eutrophic water | |
| CN103288115B (en) | The method of impurity metal ion in multistage resin column removing liquor alumini chloridi | |
| CN108393076B (en) | Copper-containing adsorbent, preparation method and application thereof in adsorption of tetracycline in water | |
| CN102249277B (en) | Method for deironing aluminum chloride solution | |
| RU2011129684A (en) | REMOVAL OF PERCHLORATE FROM CONCENTRATED SALT SOLUTIONS USING AMPHOTERIC ION EXCHANGE RESINS | |
| CN202936209U (en) | Co-production device of salt and mirabilite by mirabilite-type brine mechanical vapor recompression method | |
| CN106086405A (en) | A kind of purifying and impurity-removing method of high salt Chloride System | |
| CN1724370A (en) | Process for producing potassium chloride by sulfate type potassium-containing halogen water | |
| CN103435077A (en) | Process for extracting lithium from brine | |
| CN108996521B (en) | Process for producing high-purity refined salt by using selective electrodialysis concentrated brine | |
| Ryabtsev et al. | Production of lithium hydroxide monohydrate from natural brine | |
| CN102642849B (en) | Method for removing magnesium in seawater potassium extraction process | |
| CN106587112A (en) | Comprehensive utilization method for brine | |
| CN105582895B (en) | A kind of high adsorption composite material for sewage disposal and preparation method thereof | |
| CN102502501A (en) | Method for extracting iodine from wet-process phosphoric acid produced from iodine-containing phosphorous ore by semi-water and bi-water method | |
| CN103992364A (en) | Separation extraction method of fondaparinux sodium |
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 | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170920 Address after: 050011 chemical industry road, Shijiazhuang chemical industry park, Hebei Patentee after: Hebei eight dimension Chemical Co., Ltd. Address before: 300401 Beichen, Tianjin Hebei University of Technology, Beichen Campus Patentee before: Hebei University of Technology |