CN1045319C - Method for preparing sodium hydroxide by brine electrolysis - Google Patents
Method for preparing sodium hydroxide by brine electrolysis Download PDFInfo
- Publication number
- CN1045319C CN1045319C CN94110856A CN94110856A CN1045319C CN 1045319 C CN1045319 C CN 1045319C CN 94110856 A CN94110856 A CN 94110856A CN 94110856 A CN94110856 A CN 94110856A CN 1045319 C CN1045319 C CN 1045319C
- Authority
- CN
- China
- Prior art keywords
- salt
- bittern
- sodium hydroxide
- nitre
- brine
- 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.)
- Expired - Fee Related
Links
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 title claims abstract description 92
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000012267 brine Substances 0.000 title claims abstract description 21
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 19
- 150000003839 salts Chemical class 0.000 claims abstract description 47
- 241001131796 Botaurus stellaris Species 0.000 claims abstract description 37
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 28
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000007667 floating Methods 0.000 claims abstract description 20
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 14
- 239000006227 byproduct Substances 0.000 claims abstract description 9
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- 230000008020 evaporation Effects 0.000 claims abstract description 8
- 230000008014 freezing Effects 0.000 claims abstract description 7
- 238000007710 freezing Methods 0.000 claims abstract description 7
- 239000003513 alkali Substances 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 238000007670 refining Methods 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 239000000126 substance Substances 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 235000002639 sodium chloride Nutrition 0.000 claims description 51
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 27
- 229910052736 halogen Inorganic materials 0.000 claims description 18
- 150000002367 halogens Chemical class 0.000 claims description 18
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 13
- 239000012266 salt solution Substances 0.000 claims description 10
- 239000013078 crystal Substances 0.000 claims description 9
- 239000011780 sodium chloride Substances 0.000 claims description 9
- 238000004062 sedimentation Methods 0.000 claims description 7
- 239000011734 sodium Substances 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 238000002425 crystallisation Methods 0.000 claims description 5
- 230000008025 crystallization Effects 0.000 claims description 5
- 230000009615 deamination Effects 0.000 claims description 5
- 238000006481 deamination reaction Methods 0.000 claims description 5
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 241000209094 Oryza Species 0.000 claims description 4
- 235000007164 Oryza sativa Nutrition 0.000 claims description 4
- 150000001412 amines Chemical class 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 235000009566 rice Nutrition 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000002585 base Substances 0.000 claims description 2
- 230000007935 neutral effect Effects 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 12
- 238000005516 engineering process Methods 0.000 abstract description 2
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 abstract 2
- 235000010333 potassium nitrate Nutrition 0.000 abstract 2
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 238000005065 mining Methods 0.000 abstract 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 208000034189 Sclerosis Diseases 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The present invention belongs to the technical field of the production technology of sodium hydroxide, which relates to a method for preparing the sodium hydroxide by the electrolysis of whole bittern. In the method, underground caldo is exploited in a hydraulic mining method, and saltpeter in the bittern is removed in a freezing method to prepare refined bittern; salt as the side product generated in the following production process is added in the refined bittern after the saltpeter is removed, so the bittern achieves supersaturation, inorganic ammonia and organic ammonia are removed by heating the bittern to a high temperature and adding a deaminizating agent, and floating salt is removed by a floating salt settling bucket; finally, refined brine is obtained in a chemical refining method, the liquid of the sodium hydroxide is prepared by electrolysis, evaporation, concentration and the separation between the salt and alkali, and the salt as the side product can be circulated fro the supersaturation of the refined bittern. With the utilization of the method of the present invention, the sodium hydroxide can be produced from the whole bittern.
Description
The invention belongs to the production technical field of sodium hydroxide, is a kind of method with preparing sodium hydroxide by brine electrolysis.
Industrial employing electrolytic process is produced caustic soda and chlorine has long history, and traditional production method mainly is to utilize sea salt to be dissolved into saturated brine electrolysis production sodium hydroxide and chlorine again.In recent years because sea salt transportation difficulty, cause the cost up with this explained hereafter NaOH, some producer's employing is at present mixed halogen technology and is reduced production costs, and mixes the halogen ratio and is 50% to the maximum, because it is different that the bittern mineral products are formed because of the region is different, resemble that to contain nitre in the bittern on ground such as Sichuan be saltcake (Na
2SO
4) amount very little, can reach about 30 grams per liters and contain the nitre amount in the salt mine bittern on ground such as Hubei, Hunan, sulfate ion content is bigger, and is very big to electrolytic influence, therefore with contain caldo mix halogen particularly perhalogeno system alkali, except that nitre, except that difficult problems such as ammonia are difficult to capture, can't realize making alkali production.
The method that the objective of the invention is to provide a kind of usefulness to contain the nitre preparing sodium hydroxide by brine electrolysis, make full use of the local caldo resource that contains, reduce production costs.
The objective of the invention is to realize with the following methods.The method that this usefulness contains the nitre preparing sodium hydroxide by brine electrolysis is from underground extraction with bittern, obtain thick bittern, thick bittern is cooled to after 5-25 ℃ through interchanger, add the freezing bittern temperature adjustment to 0 ℃ of band nitre through converting the halogen groove, send into crystallizer, 0-25 ℃ of freezing denitration down, making sodium chloride crystal is solid, contain the crystallization caldo and crystal is grown up and sedimentation crystal nitre, obtain to contain NaCL270-290 grams per liter, Na through settling vat
2SO
46.5 the smart halogen that grams per liter is following, smart halogen carries out heat exchange with thick halogen in interchanger, smart halogen temperature is raise, thick brine temperature reduces, in smart bittern, add the by-product salt that the back evaporation section obtains then, make smart bittern reach supersaturation, heating supersaturated brine to 100 ℃ high temperature, add deamidization, make organic amine transfer inorganic ammonia to, inorganic ammonia in the supersaturated brine at high temperature volatilizees, and reaches salt solution and contains below ammonia 1 mg/litre, and adjusting deamination salt water ph value with acid is neutral about PH7, send floating salt settling bucket to remove floating salt only then, adopt the chemical refining method to obtain saliferous 315-320 grams per liter again, Ca
++, Mg
++(the refined brine that 10 mg/litre are following, refined brine carries out electrolysis after preheating, with the alkali lye that obtains after the electrolysis carry out evaporation concentration, saline and alkaline separation, salt is analysed in cooling, the salt of separating out is used for the supersaturation of smart bittern as by-product salt, obtaining liquid caustic soda at last is sodium hydroxide.
In the present invention, settling vat that heavy nitre is used adopts the inclined plate sedimentation bucket, utilizes gravity settling crystallization nitre, and the deamidization that adds in the supersaturated brine is a clorox, and the organic amine reaction production inorganic ammonia in clorox and the salt solution is easy to volatilize.Adjusting the used acid of deamination salt water ph value with acid is hydrochloric acid.Saturated brine (310-315 grams per liter) after heavy nitre and the deammoniation is owing to contain a large amount of floating salt, its particle surface adheres to one deck alkali film, easily build up the sclerosis caking, the clog up process equipment pipeline, cause producing and to carry out, to dissolve the floating salt that by-product salt (producing supersaturation bittern) that evaporation section reclaims produces be compact crystal type and unformed powder by containing the smart bittern of NaCL270-290 grams per liter, granulometric range is at 200-1500 μ, dissolution rate is slow, among the present invention, the clean method of removing floating salt is to adopt floating salt settling bucket, obtains good result by the mode of filtering with gravity settling.The floating similar Dao Er type of salt settling bucket settling tank, in establish central canal, divide into the mud layer fillter section, top is back taper type expanding reach, the floating salt loading salt solution that enters central canal is adjusted pH value in advance and is slight alkalinity, salt solution enters the macrobead filtering of mud layer fillter section with 800-1500 μ from central canal base cone portion, the 200-800 μ particle that sees through mud layer rises to expanding reach, because the particulate settling velocity is generally greater than in 0.6-1.0 rice/time scope, and expanding reach salt solution lift velocity sky relies on gravity settling to remove particulate clean only within 0.3-0.4 rice/time.In order to reach the good result of equipment, the strict insulation of floating salt settling bucket outer wall prevents that the convection current of the liquid phase temperature difference from influencing sedimentation, and is fixed in bucket for preventing particle, and the outer pH value that is provided with of bucket is adjusted supplementary unit and bucket end cleaning plant.
Embodiment:
In the somewhere, Hunan with the hydromining method with bittern from underground extraction, obtain to contain about 270 grams per liters of NaCL, Na
2SO
4The thick bittern of 25 grams per liters, thick bittern is cooled to 15 ℃ through interchanger, adds-10 ℃ freezing bittern of band nitre with extremely about 0 ℃ of thick bittern temperature adjustment through converting the halogen groove.Send into crystallizer decrease temperature crystalline, freezing under-12 ℃, making sodium chloride crystal is solid, and the bittern that contains solid nitre grows up crystal through first settling vat and second settling vat (first, second settling vat all adopts the inclined plate sedimentation bucket), utilizes the gravity settling crystallization to be Na
2SO
4H
2O nitre obtains to contain Na behind the heavy nitre
2The CL270-290 grams per liter, Na
2SO
46.5 the smart halogen that grams per liter is following, smart halogen is carried out heat exchange with thick bittern that exploitation is come out in heat exchanger, thick brine temperature reduces, smart halogen temperature is grown tall, add by-product salt that evaporation section obtains then in smart bittern, make it reach supersaturation, supersaturated brine heated after 100 ℃, add the deamidization clorox, inorganic ammonia in smart halogen at high temperature volatilizees, organic amine and sodium hypochlorite reaction and generate inorganic ammonia and volatilize, reaching salt solution like this contains below ammonia 1 mg/litre, adjusting deamination salt water ph value with hydrochloric acid is neutrality (PH7), send then and floats the salt settling bucket only except that floating salt, carries out chemical refining except that adding Na2CO3 after the floating salt only, acquisition contains NaCL315-320 grams per liter, Ca
++, Mg
++The refined brine that meets the electrolysis requirement below＜10 mg/litre, send into electrolytic tank electrolysis, the electrolytic lye that flows out electrolyzer contains NaOH10-11%, stores at the electrolytic lye storage tank, concentrates with being pumped into evaporation unit, make 30%, 42%, 50% liquid caustic soda, divide salt through minute salt device or whizzer, after the saline and alkaline separation, liquid caustic soda is gone into storage tank and is cooled off heavy clear once more, after further analysing salt, be the liquid caustic soda finished product.Isolating by-product salt is capable of circulation, and to be used for smart bittern saturated again.
The inventive method whole production flow process has adopted 1, the cooling denitration, and 2, remove ammonia, 3, saturated again, 4, floating salt sedimentation process for refining step, make refined brine reach the standard that enters electrolyzer, satisfy the requirement of producing chlorine, hydrogen, caustic soda.The production process of the inventive method is all utilized the underground cheap bittern resource of China's abundant, do not need to add in addition sea salt or other Industrial Salt, reduce production costs, caustic soda per ton (100%NaOH) about 500 yuan of the salt cost (in January, 94 price) that can economize in raw materials makes manufacturer can obtain good economic benefits.
Claims (5)
1, a kind of usefulness contains the method for nitre preparing sodium hydroxide by brine electrolysis, it is characterized in that bittern from underground extraction, obtain thick bittern, thick bittern is cooled to after 5-25 ℃ through interchanger, adds the freezing bittern temperature adjustment of band nitre to about 0 ℃ through converting the halogen groove, send into crystallizer, 0-25 ℃ of freezing denitration down, making sodium chloride crystal is solid, contains the crystallization caldo through settling vat crystal to be grown up and sedimentation crystal nitre, acquisition contains NaCL270-290 grams per liter, Na
2SO
46.5 the smart halogen that grams per liter is following, smart halogen carries out heat exchange with thick halogen in interchanger, smart halogen temperature is raise, thick brine temperature reduces, in smart bittern, add the by-product salt that the back evaporation section obtains then, make smart bittern reach supersaturation, the heating supersaturated brine is to about 100 ℃ of high temperature, add deamidization, make organic amine transfer inorganic ammonia to, inorganic ammonia in the supersaturated brine at high temperature volatilizees, and reaches salt solution and contains below ammonia 1 mg/litre, and adjusting deamination salt water ph value with acid is neutral about PH7, send floating salt settling bucket to remove floating salt only then, adopt the chemical refining method to obtain saliferous 315-320 grams per liter again, Ca
++, Mg
++The refined brine that＜10 mg/litre are following, refined brine carries out electrolysis after preheating, with the alkali lye that obtains after the electrolysis carry out evaporation concentration, saline and alkaline separation, salt is analysed in cooling, the salt of separating out is used for the supersaturation of smart bittern as by-product salt, obtaining liquid caustic soda at last is sodium hydroxide.
2, usefulness according to claim 1 contains the method for nitre preparing sodium hydroxide by brine electrolysis, it is characterized in that the deamidization that adds in supersaturated brine is a clorox.
3, usefulness according to claim 1 contains the method for nitre preparing sodium hydroxide by brine electrolysis, it is characterized in that adjusting the used acid of deamination salt water ph value with acid is hydrochloric acid.
4, usefulness according to claim 1 contains the method for nitre preparing sodium hydroxide by brine electrolysis, it is characterized in that the settling vat that heavy nitre is used adopts the inclined plate sedimentation bucket, utilizes gravity settling crystallization nitre.
5, usefulness according to claim 1 contains the method for nitre preparing sodium hydroxide by brine electrolysis, it is characterized in that removing floating salt only with floating salt settling bucket, the floating similar Dao Er type of salt settling bucket settling tank, in establish central canal, divide into the mud layer fillter section, top is back taper type expanding reach, the floating salt loading salt solution that enters central canal is adjusted pH value in advance and is slight alkalinity, salt solution enters the macrobead filtering of mud layer fillter section with 800-1500 μ from central canal base cone portion, the 200-800 μ particle that sees through mud layer rises to expanding reach, because the particulate settling velocity is generally greater than in 0.6-1.0 rice/time scope, and expanding reach salt solution lift velocity was controlled within 0.3-0.4 rice/time, relied on gravity settling will float the salt particulate and removed clean only.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94110856A CN1045319C (en) | 1994-03-03 | 1994-03-03 | Method for preparing sodium hydroxide by brine electrolysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94110856A CN1045319C (en) | 1994-03-03 | 1994-03-03 | Method for preparing sodium hydroxide by brine electrolysis |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1107903A CN1107903A (en) | 1995-09-06 |
| CN1045319C true CN1045319C (en) | 1999-09-29 |
Family
ID=5034774
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN94110856A Expired - Fee Related CN1045319C (en) | 1994-03-03 | 1994-03-03 | Method for preparing sodium hydroxide by brine electrolysis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1045319C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1309871C (en) * | 2002-03-28 | 2007-04-11 | 韩化石油化学株式会社 | Electrolyte composition for electrolysis of brine, method for electrolysis of brine, and sodium hydroxide prepared therefrom |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101787541B (en) * | 2010-01-26 | 2011-08-17 | 四川金路集团股份有限公司 | Method for removing nitrates through CIM membrane method |
| CN102344219B (en) * | 2011-07-04 | 2013-01-30 | 四川省乐山市福华通达农药科技有限公司 | Method of total halogenated caustic production |
| CN102851684B (en) * | 2012-09-17 | 2015-08-05 | 广州新普利节能环保科技有限公司 | A kind of perhalogeno water function of mechanical steam recompression method alkali-making process and device |
| CN107022770B (en) * | 2017-04-28 | 2019-04-26 | 湖北可赛化工有限公司 | A kind of process system and method for high caldo perhalogeno ionic membrane alkaline |
| CN110723742A (en) * | 2019-11-26 | 2020-01-24 | 江西富达盐化有限公司 | Novel process for producing liquid salt by using sodium carbonate distillate |
| CN111943232B (en) * | 2020-08-12 | 2023-03-17 | 暨南大学 | Salt-nitrate separation system and frozen nitrate production method using same |
| CN117623341A (en) * | 2023-11-29 | 2024-03-01 | 上海言征分离技术有限公司 | A quantitative dosing method and system for industrial wet salt particles |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5339773A (en) * | 1976-09-24 | 1978-04-11 | Hitachi Ltd | Liquid level detector |
| US4246201A (en) * | 1979-06-11 | 1981-01-20 | Alfa Farmaceutici, S.P.A. | Substituted N-(3-phenylthiopropyl)-3,3-diphenyl-propylamines possessing pharmacological activity |
| CN1033782A (en) * | 1987-12-30 | 1989-07-12 | 中南工业大学 | A kind of method that purifies sodium sulphate type bittern |
-
1994
- 1994-03-03 CN CN94110856A patent/CN1045319C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5339773A (en) * | 1976-09-24 | 1978-04-11 | Hitachi Ltd | Liquid level detector |
| US4246201A (en) * | 1979-06-11 | 1981-01-20 | Alfa Farmaceutici, S.P.A. | Substituted N-(3-phenylthiopropyl)-3,3-diphenyl-propylamines possessing pharmacological activity |
| CN1033782A (en) * | 1987-12-30 | 1989-07-12 | 中南工业大学 | A kind of method that purifies sodium sulphate type bittern |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1309871C (en) * | 2002-03-28 | 2007-04-11 | 韩化石油化学株式会社 | Electrolyte composition for electrolysis of brine, method for electrolysis of brine, and sodium hydroxide prepared therefrom |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1107903A (en) | 1995-09-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5283054A (en) | Process for producing sodium salts from brines of sodium ores | |
| CN1315730C (en) | Getting alkali from salt solution and calcining sesquicarbonate of soda | |
| US3970528A (en) | Process for the purification of electrolysis brine | |
| CN1042824C (en) | Method of preparing of sodium salt from water containing sodium mineral | |
| CN218561161U (en) | Low-cost high salt mine water evaporation crystallization system | |
| EP0498919B1 (en) | Purification of chlor-alkali membrane cell brine | |
| CN105236450A (en) | Total-circulation clean production process of baking soda through double decomposition reaction | |
| CN1045319C (en) | Method for preparing sodium hydroxide by brine electrolysis | |
| US4839003A (en) | Process for producing alkali hydroxide, chlorine and hydrogen by the electrolysis of an aqueous alkali chloride solution in a membrane cell | |
| CN116281906A (en) | Method for efficiently utilizing high-purity lithium carbonate mother liquor | |
| EP0427972B1 (en) | Purification of chlor-alkali membrane cell brine | |
| JP4555227B2 (en) | Simultaneous recovery of edible salt enriched with potassium chloride and KCl | |
| CN102092880B (en) | Process for freezing and denitriding primary brine with membrane method in polyvinyl chloride production | |
| CN101108738A (en) | Manufacturing technique of potassium muriate heat of evaporation separating cooling crystallization process | |
| CN1150120A (en) | Process for producing alkali and potassium sulfate from bittern containing sulfate | |
| CN1133586C (en) | Cold separation and carbonization process for preparing sodium carbonate from natural soda | |
| CN1179882C (en) | Process for preparing potassium sulfate | |
| CN105366698B (en) | A kind of preparation method of Magnesium sulfate heptahydrate | |
| CN1151968A (en) | Crystallization technology for producing sodium chloride | |
| CN100368298C (en) | Method for preparing strontium carbonate in high purity from celestite ore in mid and low grades | |
| CN117618972A (en) | Environment-friendly disposal system and method for sodium sulfate mixed salt in lithium carbonate industry | |
| CN1033782A (en) | A kind of method that purifies sodium sulphate type bittern | |
| CN203668163U (en) | Device for nitrate removal by membrane method | |
| CN86102308A (en) | Process for preparing powdered tungstic acid from tungsten concentrate | |
| CN87101977A (en) | The technology of Vanadium Pentoxide in FLAKES is extracted in enrichment from contain the vanadium dilute solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |