CN1025727C - A new method for preparing potassium chloride from chloride-type potassium-containing brine - Google Patents
A new method for preparing potassium chloride from chloride-type potassium-containing brine Download PDFInfo
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- CN1025727C CN1025727C CN 92107304 CN92107304A CN1025727C CN 1025727 C CN1025727 C CN 1025727C CN 92107304 CN92107304 CN 92107304 CN 92107304 A CN92107304 A CN 92107304A CN 1025727 C CN1025727 C CN 1025727C
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- Prior art keywords
- sodium
- carnallitite
- bittern
- repone
- point
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- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 title claims abstract description 78
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000012267 brine Substances 0.000 title claims abstract description 14
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 14
- 239000001103 potassium chloride Substances 0.000 title claims abstract description 13
- 235000011164 potassium chloride Nutrition 0.000 title claims abstract description 13
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 239000011591 potassium Substances 0.000 title claims abstract description 12
- 229910052700 potassium Inorganic materials 0.000 title claims abstract description 12
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 34
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 26
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 claims abstract description 26
- 239000011734 sodium Substances 0.000 claims abstract description 24
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 23
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 claims abstract description 19
- 239000011780 sodium chloride Substances 0.000 claims abstract description 17
- 239000002245 particle Substances 0.000 claims abstract description 16
- 239000013505 freshwater Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 239000012452 mother liquor Substances 0.000 claims abstract description 8
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 7
- 241001131796 Botaurus stellaris Species 0.000 claims description 76
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 24
- 150000003839 salts Chemical class 0.000 claims description 21
- 229910052736 halogen Inorganic materials 0.000 claims description 18
- 150000002367 halogens Chemical class 0.000 claims description 18
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 claims description 16
- 238000005406 washing Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 9
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 7
- 230000003760 hair shine Effects 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 159000000000 sodium salts Chemical class 0.000 claims description 4
- 238000005695 dehalogenation reaction Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000009413 insulation Methods 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 238000007670 refining Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 abstract description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract description 2
- 239000013078 crystal Substances 0.000 abstract 1
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 abstract 1
- 238000002425 crystallisation Methods 0.000 description 15
- 230000008025 crystallization Effects 0.000 description 14
- 238000009826 distribution Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 229910052599 brucite Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005188 flotation Methods 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
- -1 washing method Chemical compound 0.000 description 1
Images
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
A novel method for preparing potassium chloride from chloride type potassium-containing brine is characterized in that carnallite point brine and bischofite point brine are mixed according to the weight ratio of 1: 1-1: 3, the mixture is fully stirred and reacted for more than 15 minutes, the obtained artificial carnallite and sodium chloride are subjected to fractional separation and sodium removal according to particle size difference, then low-sodium carnallite, fresh water and decomposition mother liquor are continuously and uniformly added into a crystallizer according to the proportion, 300-800 kg of low-sodium carnallite is added per cubic meter per hour, and fully-mixed flow is continuously and uniformly stirred to obtain potassium chloride crystals with larger particles, so that the influence of natural environment and potassium salt stage sodium removal on yield and quality is eliminated, the cost is low, the grade is over 96%, the total yield is high, and no pollution is caused.
Description
The present invention relates to a kind of is the method that raw material is made Repone K with the potassium chloride-type brine.
In the prior art, potassium chloride-type brine shines through the beach, salt pan, general crystallization rule is, evaporation along with moisture content, bittern begins precipitated sodium chloride after reaching the saturation point of sodium-chlor earlier, and moisture content further evaporates, after bittern reaches the common saturation point of sodium-chlor, Repone K and carnallitite, after promptly reaching carnallitite point bittern, begin to separate out the carnallitite (Kcl.Mgcl of the inhomogeneous random distribution of granularity
2.6H
2O), moisture content continues evaporation, and bittern reaches sodium-chlor, carnallitite and bischofite (Mgcl
2.6H
2O) after the common saturation point, and after reaching bischofite point bittern, begin to separate out bischofite.According to this characteristic, publish in September, 1988 as Chemical Industry Press, Xie Weijie chief editor's " chemical fertilizer industry complete works ", having introduced existing is the method that raw material is made Repone K with the potassium chloride-type brine, be from gathering bittern, ted by the salt pan sodium-chlor is separated out, according to temperature control bittern composition, reach sodium-chlor, separate sodium-chlor during the common saturation point of Repone K and carnallitite and make carnallitite point bittern, carnallitite is put bittern continuation beach to be shone to brucite point bittern, the carnallitite crystallization is separated out, again brucite is put bittern and separated, obtain the carnallitite (Kcl.Mgcl that contains sodium-chlor of the inhomogeneous random distribution of granularity
2.6H
2O), use it again, after sloughing magnesium chloride and obtain sylvite through cold decomposition earlier, slough sodium-chlor, wash again and make Repone K with following method as raw material:
1, dissolve and wash away with a large amount of fresh water and slough sodium-chlor, i.e. washing method, the poor product quality that obtains, grade, yield are very low, fine size.
2, with fatty amine medicament sodium-chlor is separated and to improve product grade, it is flotation process, its smart potassium product potential energy reaches 90%, in the carnallitite product yield is 65%, is 55% in carnallitite point bittern total recovery, but the finely powdered product granularity that obtains is too thin, cause dehydration, drying, processing, the inconvenience when using, and contain flotation reagent and be difficult to use in industrial production.
The different solubility of Repone K and sodium-chlor separates sodium-chlor when 3, utilizing differing temps, i.e. thermosoling, but the production process energy consumption is big, and strong to equipment corrosion, facility investment and production cost are very high.
The suitable crystallization condition of control makes oarse-grained Repone K crystallization during 4, with the cold decomposition of sodium-containing carnallite, in special cooling crystallizer, utilize particle size differences to separate sodium-chlor, it is the cold crystallization method, it also is the state-of-the-art method that is known as in the world at present, the Dead Sea that is used for Israel at present, but this method is to the ingredient requirement height, and technology and the necessary import of main equipment, and price is very expensive.
In sum, in the prior art, carnallitite is to be tedded by the salt pan to make, and its quality is subjected to effect of natural conditions very big, especially for high latitude land plateau area, because of effect of natural conditions, in the sodium-containing carnallite, its Repone K is about 1～1.5 with the content ratio of sodium-chlor, granularity is irregular distribution, and contain a large amount of insoluble substances, and the Repone K quality product is descended, yield is low; Moreover, slough sodium-chlor from the sylvite stage, make a large amount of Repone K enter that decomposition nut liquid is separated together goes out, cause the Repone K product yield to descend significantly.
The present invention is directed to the deficiencies in the prior art, proposed a kind of effect of natural conditions that is not subjected to, not tractable sylvite stage in the cancellation production process, the novel method of the manufacturing high-quality Repone K that grain size number is big, content is high, yield is high.
Task of the present invention is to realize like this, the present invention be a kind of be the method that raw material is made Repone K with the potassium chloride-type brine, the bittern of gathering is shone through the beach, salt pan, composition according to phasor control bittern reaches sodium-chlor, separate sodium-chlor during the common saturation point of Repone K and carnallitite, make carnallitite point bittern, make Repone K with carnallitite point bittern, carnallitite is put bittern and bischofite point bittern to be converted by weight about 1: 1～1: 3 ratio and closes, and fully stir, controlling reaction time is no less than 15 minutes, the synthetic carnallite of halogen generation and the particle diameter difference of sodium-chlor are converted in utilization, fractional separation, slough sodium-chlor, with the Repone K that obtains and sodium chloride content than the low-sodium carnalite and the fresh water that are not less than 5, decomposition nut liquid, add crystallizer continuously equably, useful volume by crystallizer, the input speed of control low-sodium carnalite per hour adds 300～800 kilograms at every cubic metre, adding the fresh water amount is as the criterion so that carnallitite is decomposed fully, decomposition nut liquid is that the weight ratio in carnallitite and decomposition nut liquid is that 1: 3～6 ratio adds, and carry out complete mixing flow and evenly stir continuously, the decomposition rate of control carnallitite, larger particles Repone K crystallizes out from liquid, dehalogenation after filtration, magnesium chloride and remaining sodium-chlor are separated with decomposition nut liquid, promptly made Repone K.
Faster in the carnallitite crystalline speed of growth of converting the halogen process than sodium-chlor crystallization, carnallitite crystalline particle is bigger than sodium-chlor crystallization, utilize this characteristic with sodium-chlor crystallization fractional separation, just can obtain Repone K and sodium chloride content than the low-sodium carnalite that is not less than 5, like this, again low-sodium carnalite is decomposed with fresh water and decomposition nut liquid, according to the Nernst equation, in conjunction with various factors of the present invention, draw the decomposition rate of carnallitite and feeding intake of carnallitite, add water speed, the saturation ratio of solution, the system solid-to-liquid ratio is relevant, as long as promptly controlling carnallitite feeds intake and adds water speed, utilize Recycling Mother Solution to make the degree of supersaturation of decline of system solid-to-liquid ratio and reduction solution, and complete mixing flow fully stirs to prevent local supersaturation generation, i.e. may command decomposition rate.And test-results shows, as long as the control decomposition rate separates magniferous mother liquor, just can obtain the high-quality Repone K crystallization that content reaches 90～95% larger particles.
Carnallitite is put bittern and bischofite point bittern to be converted the process of closing and places in the container and carry out.Convert halogen with container and can effectively control reaction conditions, to guarantee the stable of carnallitite quality.
The temperature difference that carnallitite point bittern and bischofite point bittern are converted fashionable two kinds of bittern preferably is no less than 10 ℃.The method that improves the carnallitite point bittern and the bischofite point bittern temperature difference places the beach, shallow water salt pan of carnallitite place mat to shine when daily temperature rises for carnallitite being put bittern, when daily temperature is crossed vertex and is begun to descend, place deep water salt pond insulation, and bischofite point bittern is gathered will avoid day high temperature the time.Carnallitite is put bittern and bischofite point bittern, and to convert the process of closing be to carry out being aided with under the condition of cooling.The temperature difference is converted halogen and is aided with the cooling means and the yield of carnallitite can be improved 8～15%.
Repone K drip washing in filter plant with making is drying to obtain refined potassium chloride through solid-liquid separation.This process mainly is to slough remaining magnesium chloride, rather than unmanageable sodium-chlor, is 96～99.5% Repone K so the Repone K that the present invention produces also only needs simple means can obtain content at refining stage.
The present invention compared with prior art, owing in converting the halogen process, slough sodium-chlor, produce Repone K and sodium chloride content than the low-sodium carnalite that is not less than 5, carnallitite quality height not only, also remove the beach, salt pan from and shone the inconvenience that carnallitite fells and transports and processes, got rid of the influence of physical environment to Repone K product yield and quality, also got rid of the influence to Repone K yield and quality when sloughing sodium-chlor of sylvite stage in the prior art production process, make and take off the sodium process and become than being easier to, only lose a spot of Repone K, and the Repone K in the recyclable bischofite point bittern; The decomposition rate of control carnallitite is sloughed magnesium chloride and remaining sodium-chlor process operation is simple, does not relate to temperature, pressure.After making Repone K, treating process also is based on de-magging, thereby treating process technology is also simple.In the whole process, do not consume heat energy, also do not need cost height, complex apparatus, initial cost is low.Through adjusting, production cost is lower than various prior aries.Obtain white granular Repone K elaboration position between 96～99.5%, and do not contain any medicament; In the carnallitite is that the raw material product yield is greater than 80%; In carnallitite point bittern is that the raw material total recovery is greater than 63%; Product cut size is greater than 0.4 millimeter, and its quality is higher than GB industry first class product.And all mother liquors all can be recycled or reclaim, and do not have old halogen and tail salt to discharge, and can not pollute environment.
Fig. 1 is a technological process block-diagram of the present invention.
Fig. 2 is 15 ℃ " K
+, Na
+, Mg
++/ cl-H
2O, " the system isothermal phase diagram.
Among Fig. 2, in the time of 15 ℃, the E point is the phase point of carnallite point bittern, the F point is the phase point of shepardite point bittern, it is along with the minimizing of the water content common saturated line crystallization along sodium chloride and carnallite basically that the bittern that shine on normal beach, salt pan reaches behind the carnallite point bittern, thereby the carnallite sodium chloride-containing that obtains is higher, forms the M point and convert the total material of finishing liquid that closes with carnallite point bittern and bischofite point bittern, drops on carnallite (Kcl.Mgcl2.6H
2O) on the crystallization curved surface, carnallite is separated out in reaction, liquid phase forms some P and moves on the common saturated line of carnallite and sodium chloride, the while precipitated sodium chloride, the speed of growth of carnallite crystallization is faster than sodium chloride crystallization, and the particle of carnallite crystallization is bigger than sodium chloride crystallization, like this, the sodium chloride of classification separate small particles can obtain the low-sodium carnalite of high-quality.
Embodiment one: present embodiment in conjunction with the accompanying drawings, among the figure is the method that raw material is made Repone K with the potassium chloride-type brine, be that the bittern that will gather shines through sodium salt Chi Tan, composition proportion according to phasor control bittern restrains about every cubic centimetre 1.27, reach sodium-chlor, separate sodium-chlor during the common saturation point of Repone K and carnallitite, make carnallitite point bittern, carnallitite is selected brine pump to carnallitite order the halogen equalizing tank, be under 15 ℃ the condition at normal temperature, carnallitite is put bittern and bischofite point bittern to be placed container to convert by weight about 1: 2 ratio to close, and fully stir, controlling reaction time was at 15 minutes, the synthetic carnallite of halogen generation and the particle diameter difference of sodium-chlor are converted in utilization, according to stokes sedimentation law, in conjunction with various factors of the present invention, the settling velocity of suspended particles and its particle dia square is directly proportional in the solution, thereby the settling velocity of carnallitite is also faster than sodium-chlor, fractional separation, slough particle diameter less than 0.097 millimeter sodium-chlor, with the Repone K that obtains and sodium chloride content than the low-sodium carnalite and the fresh water that are not less than 5, decomposition nut liquid, be about 1: 0.5: 4 ratio by weight, evenly add crystallizer continuously, useful volume by crystallizer, the input speed of control low-sodium carnalite per hour adds 600 kilograms at every cubic metre, and carry out complete mixing flow and evenly stir continuously, control carnallitite decomposition rate, particle diameter is not less than 0.4 millimeter macrobead Repone K and ties scape come out from liquid, dehalogenation after filtration, magnesium chloride and remaining sodium-chlor are separated with decomposition nut liquid, promptly made content and be 93% Repone K.The content that makes is about Repone K simple drip washing in filter plant of 93%, and the weight of leacheate is 80～100% of thick potassium, and leacheate is made into by 1: 1 weight ratio by drip washing mother liquor and fresh water, is drying to obtain content through solid-liquid separation and is about 98% refined potassium chloride.Like this, reach 85% with the carnallitite rate of collecting.To select bittern be that the gather old halogen or own solarization of other salt pans dischargings made to initial bischofite when converting halogen and taking off sodium, converting the isolated halogen mother liquor of converting of halogen process becomes bischofite point bittern again and recycles after precipitated sodium chloride, carnallitite are shone in the beach, salt pan, the secondary carnallitite of separating out returns sodium salt Chi Tan and shines recovery after the dissolving of shallow water salt pan.Low-sodium carnalite control speed is decomposed and when sloughing magnesium chloride and remaining sodium-chlor, the decomposition nut liquid of initial usefulness can obtain with fresh water drip washing carnallitite, controls the decomposition nut liquid that fast decomposition and separation goes out and partly recycles, and remainder returns converts halogen production low-sodium carnalite.Initial only need of drip washing mother liquor when drip washing is refining can obtain with the thick potassium of fresh water drip washing, and isolated drip washing mother liquor partly recycles in the lessivation, and remainder returns the solarization of beach, salt pan and reclaims.The Recycling Mother Solution use of each process can further be improved product yield, also avoided environmental pollution.Like this, the grade of the refined potassium chloride that obtains reaches 98%, reaches 95% in the carnallitite product yield, reaches 68% in carnallitite point bittern total recovery.
Embodiment two: present embodiment, in conjunction with the accompanying drawings, among the figure is the method that raw material is made Repone K with the potassium chloride-type brine, be that the bittern that will gather shines through sodium salt Chi Tan, composition proportion according to phasor control bittern restrains about every cubic centimetre 1.27, separate sodium-chlor when reaching the common saturation point of sodium-chlor, Repone K and carnallitite, make carnallitite point bittern, carnallitite is selected brine pump to carnallitite order the halogen equalizing tank, the temperature difference that carnallitite point bittern and bischofite point bittern are converted fashionable two kinds of bittern is 10 ℃.The method that improves the carnallitite point bittern and the bischofite point bittern temperature difference places the shallow water salt pan of carnallitite place mat to ted when daily temperature rises for carnallitite is put bittern, when daily temperature is crossed vertex and is begun to descend, place deep water salt pond insulation, and bischofite point bittern is gathered will avoid day high temperature the time.Being that carnallitite is put bittern and bischofite point bittern, to convert the process of closing be to use open container, and by carrying out under the ventilative condition that is aided with cooling of sunshade.The embodiment of back process is with embodiment one.Like this, the grade of the refined potassium chloride that obtains reaches 98%, reaches 95% in the carnallitite product yield, reaches 80% in carnallitite point bittern total recovery.
Claims (9)
1, a kind of is the method that raw material is made Repone K with the potassium chloride-type brine, the bittern of gathering is shone through the beach, salt pan, evaporation along with moisture content, bittern begins precipitated sodium chloride after reaching the saturation point of sodium-chlor earlier, moisture content further evaporates, reach sodium-chlor, the common saturation point of Repone K and carnallitite, separate sodium-chlor, make carnallitite point bittern, make Repone K with carnallitite point bittern, it is characterized in that carnallitite is put bittern and bischofite point bittern to be converted by weight about 1: 1～1: 3 ratio and close, and fully stir, controlling reaction time is no less than 15 minutes, the synthetic carnallite of halogen generation and the particle diameter difference of sodium-chlor are converted in utilization, fractional separation, slough sodium-chlor, with the Repone K that obtains and sodium chloride content than the low-sodium carnalite and the fresh water that are not less than 5, decomposition nut liquid, add crystallizer continuously equably, useful volume by crystallizer, the input speed of control low-sodium carnalite per hour adds 300～800 kilograms at every cubic metre, adding the fresh water amount is as the criterion so that carnallitite is decomposed fully, decomposition nut liquid is that the weight ratio in carnallitite and decomposition nut liquid is that 1: 3～6 ratio adds, and carry out complete mixing flow and evenly stir continuously, the decomposition rate of control carnallitite, larger particles Repone K crystallizes out from liquid, after filtration dehalogenation, magnesium chloride and remaining sodium-chlor are separated with decomposition nut liquid, promptly made Repone K.
2, the method for manufacturing Repone K according to claim 1 is characterized in that carnallitite is put bittern and bischofite point bittern to be converted the process of closing and place in the container and carry out.
3, the method for manufacturing Repone K according to claim 1 is characterized in that carnallitite point bittern and bischofite point bittern converts the temperature difference of fashionable two kinds of bittern and preferably be no less than 10 ℃.
4, according to the method for claim 1 and 3 described manufacturing Repone K, it is characterized in that the method that improves the carnallitite point bittern and the bischofite point bittern temperature difference places the beach, shallow water salt pan of carnallitite place mat to shine for carnallitite being put bittern when daily temperature rises, when daily temperature is crossed vertex and is begun to descend, place deep water salt pond insulation, and bischofite point bittern is gathered will avoid day high temperature the time.
5, according to the method for claim 1 and 3 described manufacturing Repone K, it is characterized in that carnallitite is put bittern and bischofite point bittern, to convert the process of closing be to carry out being aided with under the condition of cooling.
6,, it is characterized in that the Repone K drip washing in filter plant that to make being drying to obtain refined potassium chloride through solid-liquid separation according to the method for the described manufacturing Repone K of claim 1 to 4.
7, the method for manufacturing Repone K according to claim 1, the isolated halogen mother liquor of converting becomes bischofite point bittern again and recycles when it is characterized in that converting halogen and taking off sodium after precipitated sodium chloride, carnallitite are shone in the beach, salt pan, and the secondary carnallitite of separating out returns sodium salt Chi Tan and shines recovery after the dissolving of shallow water salt pan.
8, the method for manufacturing Repone K according to claim 1, isolated decomposition nut liquid partly recycles when it is characterized in that sloughing magnesium chloride and remaining sodium-chlor when low-sodium carnalite decomposes, and remainder returns converts halogen production low-sodium carnalite.
9, according to the method for claim 1 and 5 described manufacturing Repone K, isolated drip washing mother liquor partly recycles when it is characterized in that drip washing is refining, and remainder returns the beach, salt pan and shines and reclaim.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92107304 CN1025727C (en) | 1992-03-05 | 1992-03-05 | A new method for preparing potassium chloride from chloride-type potassium-containing brine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92107304 CN1025727C (en) | 1992-03-05 | 1992-03-05 | A new method for preparing potassium chloride from chloride-type potassium-containing brine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1063663A CN1063663A (en) | 1992-08-19 |
| CN1025727C true CN1025727C (en) | 1994-08-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92107304 Expired - Lifetime CN1025727C (en) | 1992-03-05 | 1992-03-05 | A new method for preparing potassium chloride from chloride-type potassium-containing brine |
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Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1094466C (en) * | 1999-01-04 | 2002-11-20 | 化学工业部连云港设计研究院 | Method of extracting potassium chloride from mixed ore of sylvine and carnallite |
| CN1124981C (en) * | 2000-06-22 | 2003-10-22 | 宋侑霖 | Method for directly obtaining low-sodium fine carnallitite |
| CN1304293C (en) * | 2002-10-15 | 2007-03-14 | 云南地矿勘查工程总公司(集团) | Preparation of potassium chloride by multi-component crystallization of solid mineral production by dissolving and leaching process |
| CN100402427C (en) * | 2005-06-01 | 2008-07-16 | 高崧耀 | Method for producing potassium chloride crystal through solarization on large area of brine pan |
| CN100383044C (en) * | 2005-07-25 | 2008-04-23 | 魏新俊 | Method for producing low-sodium carnallite or potassium chloride with potassium-containing brine |
| CN100335411C (en) * | 2005-07-30 | 2007-09-05 | 中蓝连海设计研究院 | Method of preparing low sodium carnallite by blending halogen |
| CN101343073B (en) * | 2008-05-12 | 2010-06-09 | 部燕茹 | Dewatering industrial stove for carnaillite hydrous chloromagnesite |
| CN102424916B (en) * | 2011-12-20 | 2015-05-13 | 石嘴山市凯瑞镁化有限公司 | Method for preparing low-sodium carnallite, sodium chloride and magnesium chloride from refined magnesium slag |
| CN104030323B (en) * | 2014-05-08 | 2015-12-30 | 青海锂业有限公司 | Beach, the salt pan solarization method that a kind of salt lake lithium liquor is recycled |
| CN104495878B (en) * | 2015-01-05 | 2016-04-27 | 格尔木康生钾业科技发展有限公司 | A kind of from high calcium abandoned mine decalcification produce the method for food-grade potassium chloride |
| CN106186006B (en) * | 2016-07-27 | 2017-08-25 | 浙江鸿浩科技有限公司 | A kind of purifying lithium chloride method |
| CN111362281B (en) * | 2020-04-23 | 2022-05-24 | 青海盐湖工业股份有限公司 | Method and system for controlling water adding amount of potassium chloride crystallizer |
| CN111470519B (en) * | 2020-05-06 | 2022-05-31 | 中国科学院青海盐湖研究所 | Method for preparing potassium chloride by using high-sodium carnallite |
| CN111362730B (en) * | 2020-05-06 | 2021-11-02 | 中国科学院青海盐湖研究所 | Method for preparing low-sodium carnallite and potassium chloride by using high-sodium carnallite |
| CN112142072B (en) * | 2020-09-27 | 2023-06-13 | 青海盐湖工业股份有限公司 | Method and system for producing potassium chloride by internal circulation brine-mixed cold crystallization |
| CN113412926A (en) * | 2021-08-03 | 2021-09-21 | 地矿集团格尔木盐湖资源开发有限公司 | Nutritional green edible salt extracted from salt lake mining area and extraction method thereof |
-
1992
- 1992-03-05 CN CN 92107304 patent/CN1025727C/en not_active Expired - Lifetime
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| Publication number | Publication date |
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| CN1063663A (en) | 1992-08-19 |
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