CN102642850A - Calcium removing method in seawater potassium extraction process - Google Patents
Calcium removing method in seawater potassium extraction process Download PDFInfo
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- CN102642850A CN102642850A CN2012101467568A CN201210146756A CN102642850A CN 102642850 A CN102642850 A CN 102642850A CN 2012101467568 A CN2012101467568 A CN 2012101467568A CN 201210146756 A CN201210146756 A CN 201210146756A CN 102642850 A CN102642850 A CN 102642850A
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Abstract
The invention discloses a calcium removing method in a seawater potassium extraction process and relates to seawater treatment with an ion exchange method. A device used for removing calcium is characterized in that a calcium removing device I is arranged in front of a potassium enrichment device, ion exchange resin in a bed layer mode is filled in the calcium removing device I, a calcium removing device II is arranged in front of an evaporation device, and ion exchange resin in a bed layer mode is filled in the calcium removing device II. The method comprises the process flows that: firstly seawater is introduced into the calcium removing device I and the calcium removing device II to be contacted with the ion exchange resin, 90% of calcium in the seawater is removed, the seawater after calcium removal is introduced into the potassium enrichment device, a potassium enrichment solution produced by the potassium enrichment device is introduced into the calcium removing device I and the calcium removing device II to be contacted with the ion exchange resin, 90% of calcium in the potassium enrichment solution is removed, the potassium enrichment solution after calcium removal is sequentially sent into the evaporation device, a crystallization device and a separation device, and finally a kali salt product is produced. The method disclosed by the invention solves the problems that calcium in the potassium enrichment solution causes the scaling of a heat exchanger, a heater and an evaporator easily, the normal operation of equipment is affected, and product quality is reduced.
Description
Technical field
Technical scheme of the present invention relates to ion exchange method handles seawater, specifically removes the method for calcium in the potassium from sea water process.
Background technology
Abundant potassium resource is arranged in the seawater, adopts the potassium ion exchanger, through suction potassium, elution process can obtain the higher solution of potassium content-Fu potassium solution, again with rich potassium solution evaporate, crystallization, separation can produce sylvite.But because of containing calcium in the seawater, with the concentration effect that influences the potassium ion exchanger, the calcium in the rich potassium solution is prone to cause interchanger, well heater, fouling of evaporator, and the equipment that influences normally moves, and reduces quality product.CN101381147 discloses sea water calcium-removing and has concentrated the method for utilizing, and is to be provided with calcium-removing device at the sea water distiling plant front end, utilizes the inorganic materials of polynuclear plane to remove calcium in the seawater.This method main purpose is to avoid in the desalting process, the reduction of the plant efficiency that causes because of knot calcium dirt.
Summary of the invention
Technical problem to be solved by this invention is: the method that removes calcium in the potassium from sea water process is provided, and the calcium that has solved in the rich potassium solution is prone to cause interchanger, well heater and fouling of evaporator, and the equipment that influences normally moves, and reduces the problem of quality product.
The present invention solves this technical problem the technical scheme that is adopted: remove the method for calcium in the potassium from sea water process, the technical process of this method is: be raw material with the seawater, at first 5～30 ℃ seawater fed the calcium-removing device I; The superficial velocity that seawater feeds the bed in the calcium-removing device I is 5～10m/h; Contact with the ion exchange resin in the calcium-removing device I, 90% calcium is removed in the seawater, and the seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that 40～60 ℃ rich potassium solution feeds the calcium-removing device II; The superficial velocity that rich potassium solution feeds the bed in the calcium-removing device II is 5～8m/h, contacts with ion exchange resin in the calcium-removing device II, and 90% calcium is removed in the rich potassium solution; Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product; Above-mentioned used ion exchange resin will be regenerated according to service condition; The said calcium-removing device I that is provided with before the potassium enriching apparatus is wherein inserted the ion exchange resin of bed form, and the ion exchange resin loadings is confirmed according to calcium contents in the seawater, handles 1m
3Seawater, consumption are 25～65kg, and the said calcium-removing device II that before evaporation unit, is provided with is wherein inserted the ion exchange resin of bed form, and the ion exchange resin loadings is confirmed according to calcium contents in the rich potassium solution, handles 1m
3Rich potassium solution, consumption is 60～120kg.
Remove the method for calcium in the above-mentioned potassium from sea water process, said ion exchange resin is strongly acidic cationic exchange resin, weakly acidic cation-exchange resin, large pores cation exchange resin or chela and resin.
Remove the method for calcium in the above-mentioned potassium from sea water process, said bed form is fixed-bed type or moving-bed type.
Remove the method for calcium in the above-mentioned potassium from sea water process, said calcium-removing device I is stainless cylindrical pad tower, is made up of the ion exchange resin of cylindrical tower shell, seawer outlet, thermowell, bed form and seawater inlet; Said calcium-removing device II is stainless cylindrical pad tower, is made up of the ion exchange resin of cylindrical tower shell, rich potassium solution outlet, thermowell, bed form and rich potassium solution inlet.
Remove the method for calcium in the above-mentioned potassium from sea water process, said seawater feeds the calcium-removing device I, is that seawater feeds the calcium-removing device I from bottom to top; Said rich potassium solution feeds the calcium-removing device II, is that rich potassium solution feeds the calcium-removing device II from bottom to top.
Remove the method for calcium in the above-mentioned potassium from sea water process; Said ion exchange resin will carry out the regenerated situation and method is according to service condition; Reach capacity 90% o'clock of exchange capacity of the calcium exchange quantity of ion exchange resin adopts intermittent mode to regenerate through s.t..
Remove the method for calcium in the above-mentioned potassium from sea water process; Wherein, The specification of said calcium-removing device I and calcium-removing device II is that those skilled in the art can know; The formation of used potassium enriching apparatus, evaporation unit, crystallization apparatus and tripping device and all operations technology all are that the present technique field is known, and used ion exchange resin is then through being purchased acquisition.
The invention has the beneficial effects as follows: the present invention is the method that removes calcium in a kind of brand-new potassium from sea water process; The calcium that has solved in the rich potassium solution is prone to cause interchanger, well heater and fouling of evaporator; The equipment that influences normally moves; Reduce the problem of quality product, therefore for being that feedstock production sylvite technology is significant with the seawater.The inventive method required equipment and material are easy to get, and cost is low, and technical process is simple, help applying.
Description of drawings
Below in conjunction with accompanying drawing and embodiment the present invention is further specified.
Fig. 1 is for removing the schematic flow sheet of the method for calcium in the potassium from sea water process of the present invention.
Fig. 2 is for removing the used calcium-removing device structural representation of method of calcium in the potassium from sea water process of the present invention.
Among the figure, 1. seawer outlet or rich potassium solution outlet, 2. thermowell, the 3. ion exchange resin of bed form, 4. tower shell, 5. seawater inlet or rich potassium solution inlet.
Embodiment
Embodiment illustrated in fig. 1 showing; The flow process that removes the method for calcium in the potassium from sea water process of the present invention is: seawater raw material → calcium-removing device I → remove calcium salt; Seawater after the deliming → potassium enriching apparatus → rich potassium solution → calcium-removing device II → remove calcium salt, rich potassium solution → evaporation unit → crystallization apparatus → tripping device → sylvite.
Embodiment illustrated in fig. 2 showing; The used calcium-removing device of method that removes calcium in the potassium from sea water process of the present invention is the cylindrical pad tower, is made up of the ion exchange resin 3 of cylindrical tower shell 4, seawer outlet or rich potassium solution outlet 1, thermowell 2, bed form and seawater inlet or rich potassium solution inlet 5.The difference of calcium-removing device I and calcium-removing device II only is: " 5 " in the calcium-removing device I and " 1 " are used separately as and are seawater inlet and seawer outlet, and to be used separately as be that rich potassium solution inlet and rich potassium solution export " 5 " in the calcium-removing device II and " 1 ".
The equal stainless head tower of formation as shown in Figure 2 of used calcium-removing device I and calcium-removing device II among following all embodiment.
Embodiment 1
Before the potassium enriching apparatus, the calcium-removing device I is set, wherein inserts the 2kgLSC100 ion exchange resin of fixed-bed type, this ion exchange resin loadings is for handling 1m
3The seawater consumption is 25kg, and the calcium-removing device II is set before evaporation unit, wherein inserts the 2kgLSC500 ion exchange resin of fixed-bed type, and this ion exchange resin loadings is for handling 1m
3Rich potassium solution, consumption is 60kg.20 ℃ of the temperature of seawater raw material; The seawater of calcic 0.40g/L feeds the calcium-removing device I from bottom to top; The superficial velocity that seawater feeds the fixed bed in the calcium-removing device I is 5m/h, seawater feeding amount 50L, and seawater contacts with the interior ion exchange resin of calcium-removing device I; Its calcium contents is reduced to 0.04g/L, and 90% calcium is removed in the seawater; Seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that the rich potassium solution of 40 ℃ calcic 3.20g/L feeds the calcium-removing device II from bottom to top; Rich potassium solution feeds the superficial velocity 5m/h of the fixed bed in the calcium-removing device II, rich potassium solution feeding amount 5L, and this richness potassium solution contacts with the interior ion exchange resin of calcium-removing device II; Its calcium contents is reduced to 0.31g/L, and the deliming rate reaches 90%.Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product.When the calcium exchange quantity of institute's spent ion exchange resin reach capacity exchange capacity 90% the time, adopt intermittent mode to regenerate through s.t..
Embodiment 2
Before the potassium enriching apparatus, the calcium-removing device I is set, wherein inserts the 2kgLSC500 ion exchange resin of moving-bed type, this ion exchange resin loadings is for handling 1m
3The seawater consumption is 45kg, and the calcium-removing device II is set before evaporation unit, wherein inserts the 2kgLSC100 ion exchange resin of moving-bed type, and this ion exchange resin loadings is for handling 1m
3Rich potassium solution, consumption is 60kg.30 ℃ of the temperature of seawater raw material; The seawater of calcic 0.40g/L feeds the calcium-removing device I from bottom to top; The superficial velocity that seawater feeds the fixed bed in the calcium-removing device I is 10m/h, seawater feeding amount 50L, and seawater contacts with the interior ion exchange resin of calcium-removing device I; Its calcium contents is reduced to 0.038g/L, and 90% calcium is removed in the seawater; Seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that the rich potassium solution of 40 ℃ calcic 3.20g/L feeds the calcium-removing device II from bottom to top; Rich potassium solution feeds the superficial velocity 7m/h of the fixed bed in the calcium-removing device II, rich potassium solution feeding amount 5L, and this richness potassium solution contacts with the interior ion exchange resin of calcium-removing device II; Its calcium contents is reduced to 0.30g/L, and the deliming rate reaches 90%.Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product.When the calcium exchange quantity of institute's spent ion exchange resin reach capacity exchange capacity 90% the time, adopt intermittent mode to regenerate through s.t..
Before the potassium enriching apparatus, the calcium-removing device I is set, wherein inserts the 2kgC500 ion exchange resin of fixed-bed type, this ion exchange resin loadings is for handling 1m
3The seawater consumption is 65kg, and the calcium-removing device II is set before evaporation unit, wherein inserts the 2kgLSC500 ion exchange resin of fixed-bed type, and this ion exchange resin loadings is for handling 1m
3Rich potassium solution, consumption is 120kg.18 ℃ of the temperature of seawater raw material; The seawater of calcic 0.60g/L feeds the calcium-removing device I from bottom to top; The superficial velocity that seawater feeds the fixed bed in the calcium-removing device I is 8m/h, seawater feeding amount 40L, and seawater contacts with the interior ion exchange resin of calcium-removing device I; Its calcium contents is reduced to 0.06g/L, and 90% calcium is removed in the seawater; Seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that the rich potassium solution of 50 ℃ calcic 3.50g/L feeds the calcium-removing device II from bottom to top; Rich potassium solution feeds the superficial velocity 8m/h of the fixed bed in the calcium-removing device II, rich potassium solution feeding amount 5L, and this richness potassium solution contacts with the interior ion exchange resin of calcium-removing device II; Its calcium contents is reduced to 0.35g/L, and the deliming rate reaches 90%.Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product.When the calcium exchange quantity of institute's spent ion exchange resin reach capacity exchange capacity 90% the time, adopt intermittent mode to regenerate through s.t..
Embodiment 4
Before the potassium enriching apparatus, the calcium-removing device I is set, wherein inserts the 2kgD152 ion exchange resin of moving-bed type, this ion exchange resin loadings is for handling 1m
3The seawater consumption is 30kg, and the calcium-removing device II is set before evaporation unit, wherein inserts the 2kgD401 ion exchange resin of moving-bed type, and this ion exchange resin loadings is for handling 1m
3Rich potassium solution, consumption is 100kg.5 ℃ of the temperature of seawater raw material; The seawater of calcic 0.38g/L feeds the calcium-removing device I from bottom to top; The superficial velocity that seawater feeds the fixed bed in the calcium-removing device I is 10m/h, seawater feeding amount 50L, and seawater contacts with the interior ion exchange resin of calcium-removing device I; Its calcium contents is reduced to 0.035g/L, and 90% calcium is removed in the seawater; Seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that the rich potassium solution of 60 ℃ calcic 3.20g/L feeds the calcium-removing device II from bottom to top; Rich potassium solution feeds the superficial velocity 7m/h of the fixed bed in the calcium-removing device II, rich potassium solution feeding amount 5L, and this richness potassium solution contacts with the interior ion exchange resin of calcium-removing device II; Its calcium contents is reduced to 0.30g/L, and the deliming rate reaches 90%.Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product.When the calcium exchange quantity of institute's spent ion exchange resin reach capacity exchange capacity 90% the time, adopt intermittent mode to regenerate through s.t..
The specification of calcium-removing device I and calcium-removing device II described in above-mentioned all embodiment is that those skilled in the art can know; The formation of used potassium enriching apparatus, evaporation unit, crystallization apparatus and tripping device and all operations technology all are that the present technique field is known, and used ion exchange resin is then through being purchased acquisition.
Claims (6)
1. remove the method for calcium in the potassium from sea water process, it is characterized in that the technical process of this method is: with the seawater is raw material, at first 5～30 ℃ seawater is fed the calcium-removing device I; The superficial velocity that seawater feeds the bed in the calcium-removing device I is 5～10m/h; Contact with the ion exchange resin in the calcium-removing device I, 90% calcium is removed in the seawater, and the seawater after the deliming feeds the potassium enriching apparatus; Potassium enriching apparatus output temperature is that 40～60 ℃ rich potassium solution feeds the calcium-removing device II; The superficial velocity that rich potassium solution feeds the bed in the calcium-removing device II is 5～8m/h, contacts with ion exchange resin in the calcium-removing device II, and 90% calcium is removed in the rich potassium solution; Rich potassium solution after the deliming is successively sent into evaporation unit, crystallization apparatus and tripping device, finally makes the sylvite product; Above-mentioned used ion exchange resin will be regenerated according to service condition; The said calcium-removing device I that is provided with before the potassium enriching apparatus is wherein inserted the ion exchange resin of bed form, and the ion exchange resin loadings is confirmed according to calcium contents in the seawater, handles 1m
3Seawater, consumption are 25～65kg, and the said calcium-removing device II that before evaporation unit, is provided with is wherein inserted the ion exchange resin of bed form, and the ion exchange resin loadings is confirmed according to calcium contents in the rich potassium solution, handles 1m
3Rich potassium solution, consumption is 60～120kg.
2. according to the method that removes calcium in the said potassium from sea water process of claim 1, it is characterized in that: said ion exchange resin is strongly acidic cationic exchange resin, weakly acidic cation-exchange resin, large pores cation exchange resin or chela and resin.
3. according to the method that removes calcium in the said potassium from sea water process of claim 1, it is characterized in that: said bed form is fixed-bed type or moving-bed type.
4.. according to the method that removes calcium in the said potassium from sea water process of claim 1; It is characterized in that: said calcium-removing device I is stainless cylindrical pad tower, is made up of the ion exchange resin of cylindrical tower shell, seawer outlet, thermowell, bed form and seawater inlet; Said calcium-removing device II is stainless cylindrical pad tower, is made up of the ion exchange resin of cylindrical tower shell, rich potassium solution outlet, thermowell, bed form and rich potassium solution inlet.
5. according to the method that removes calcium in the said potassium from sea water process of claim 1, it is characterized in that: said seawater feeds the calcium-removing device I, is that seawater feeds the calcium-removing device I from bottom to top; Said rich potassium solution feeds the calcium-removing device II, is that rich potassium solution feeds calcium device II from bottom to top.
6. according to the method that removes calcium in the said potassium from sea water process of claim 1; It is characterized in that: said ion exchange resin will carry out the regenerated situation and method is according to service condition; Reach capacity 90% o'clock of exchange capacity of the calcium exchange quantity of ion exchange resin adopts intermittent mode to regenerate through s.t..
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| CN 201210146756 CN102642850B (en) | 2012-05-14 | 2012-05-14 | Calcium removing method in seawater potassium extraction process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031443A (en) * | 2012-12-26 | 2013-04-10 | 贵州大学 | Method of dealkalizing red mud and recovering aluminum and iron |
Citations (5)
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| JPH02102779A (en) * | 1988-10-13 | 1990-04-16 | Mitsubishi Heavy Ind Ltd | Pretreatment of seawater in vaporization-type seawater desalination device |
| JPH02203986A (en) * | 1989-01-31 | 1990-08-13 | Mitsubishi Heavy Ind Ltd | Process for obtaining potable water from sea water |
| CN101381147A (en) * | 2008-10-24 | 2009-03-11 | 吴宗生 | Sea water calcium-removing concentration utilization method |
| CN102167459A (en) * | 2011-03-22 | 2011-08-31 | 天津长芦汉沽盐场有限责任公司 | Production method for desalination and comprehensive utilization of seawater |
| WO2011140613A1 (en) * | 2010-05-13 | 2011-11-17 | Clean Teq Holdings Ltd. | Water treatment process |
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2012
- 2012-05-14 CN CN 201210146756 patent/CN102642850B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02102779A (en) * | 1988-10-13 | 1990-04-16 | Mitsubishi Heavy Ind Ltd | Pretreatment of seawater in vaporization-type seawater desalination device |
| JPH02203986A (en) * | 1989-01-31 | 1990-08-13 | Mitsubishi Heavy Ind Ltd | Process for obtaining potable water from sea water |
| CN101381147A (en) * | 2008-10-24 | 2009-03-11 | 吴宗生 | Sea water calcium-removing concentration utilization method |
| WO2011140613A1 (en) * | 2010-05-13 | 2011-11-17 | Clean Teq Holdings Ltd. | Water treatment process |
| CN102167459A (en) * | 2011-03-22 | 2011-08-31 | 天津长芦汉沽盐场有限责任公司 | Production method for desalination and comprehensive utilization of seawater |
Non-Patent Citations (1)
| Title |
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| DMITRI MURAVIEV ET AL.: "《Separation and concentration of calcium and magnesium from sea water by carboxylic resins with temperature-induced selectivity》", 《REACTIVE & FUNCTIONAL POLYMERS》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031443A (en) * | 2012-12-26 | 2013-04-10 | 贵州大学 | Method of dealkalizing red mud and recovering aluminum and iron |
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