CN1062528C - Clean production of sodium chlomate - Google Patents

Clean production of sodium chlomate Download PDF

Info

Publication number
CN1062528C
CN1062528C CN98100556A CN98100556A CN1062528C CN 1062528 C CN1062528 C CN 1062528C CN 98100556 A CN98100556 A CN 98100556A CN 98100556 A CN98100556 A CN 98100556A CN 1062528 C CN1062528 C CN 1062528C
Authority
CN
China
Prior art keywords
crystallization
naalo
sodium
liquid
washing
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 - Lifetime
Application number
CN98100556A
Other languages
Chinese (zh)
Other versions
CN1226512A (en
Inventor
张懿
李佐虎
王志宽
徐霞
刘嘉澍
齐涛
邹兴
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Institute of Process Engineering of CAS
Original Assignee
Institute of Chemical Metallurgy of CAS
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Institute of Chemical Metallurgy of CAS filed Critical Institute of Chemical Metallurgy of CAS
Priority to CN98100556A priority Critical patent/CN1062528C/en
Publication of CN1226512A publication Critical patent/CN1226512A/en
Application granted granted Critical
Publication of CN1062528C publication Critical patent/CN1062528C/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Abstract

The present invention relates to a clean production method for sodium chromate, which comprises: chromite is oxidized and decomposed by an NaOH molten salt medium, and a product is leached in a high-alkalinity area; hexavalent chrome leaching liquid is synchronously cooled and crystallized so as to obtain mixed type coarse crystals of sodium chromate which comprises 10 to 20% of free NaOH and sodium aluminate and crystallized mother liquid, and a purified sodium chromate crystallizing product and coarse-crystal washing liquid are obtained by the counter-current washing purification of the coarse crystals; sodium plumbite is separated by crystallization by regulating alkali of the coarse-crystal washing liquid, and is further hydrolyzed so as to obtain a chemical pure Al2O3.3H2O product; all the crystallized mother liquid is returned to a liquid-phase oxidizing system for recycle. The high energy consumption and the complicated traditional operation of equipment of conventional crystallization by evaporating concentration is replaced by the direct cooling crystallization by high-concentration leaching liquid by the method. In addition, chromium slag can be reduced to one fourth of the original chromium slag, and a recovery rate is increased by 20%.

Description

Clean production method of sodium chromate
The invention belongs to chromium chemical industry and a method for producing chromium salt, and particularly relates to a method for producing sodium chromate.
The production of chromium salt from chromite is an important method adopted in the industry of inorganic chemical basic raw materials, the existing industrial technology at home and abroad adopts the process of high-temperature oxidation roasting and decomposition of chromite by sodium carbonate, water immersion and multistage evaporation crystallization, the chromium recovery rate is low, the pollution is serious, and the process needs to be updated urgently. The sodium hydroxide low-temperature molten salt liquid-phase oxidation reaction system for treating chromite is still in a laboratory stage at home and abroad. From seventies in Japan, the new process for extracting chromium from chromite by a molten salt oxidation method is successively researched from eighties in the United states, and in view of high reaction rate and small slag amount of the new process and the prospect of solving the pollution problem from the source, theliquid phase oxidation method is called as an epoch-making chromium production method in Japan, and great attention is paid. The Japanese chemical industry Co., Ltd and the northeast university of Japan published patents and basic works on new processes for chromite in NaOH-NaNO3The reaction process in a molten salt medium has been studied, but no operable way to achieve heterogeneous reactions and alkali-chromium separation has been found to date. Although the reported methods have been improved for many years, the treatment process of molten salt liquid phase oxidation products is changed from the original methanol method to the low-concentration medium evaporation concentration-multi-stage fractional crystallization-double salt decomposition-acidification neutralization and aluminum removal, but the concentration of NaOH medium is in two-way adjustment of high-low-high, the evaporation energy consumption is high, the end point is difficult to control, and the process equipment is complex and difficult to industrialize.
From eighties of the United states to the present, the national institute of Albanay, university of Denver and mineral Bureau, has focused on the regulation of liquid-phase oxidation and the separation of NaOH-Na by methanol method2CrO4Hair waving devicePB report, PB83-106781(1982), PB88-240529(1988), PB86-132719(1985) is shown, but the proposed reaction molten salt solidification-methanol method alkali separation-water leaching-concentration fractional crystallization-silicide aluminum removal process has high production cost, methanol is flammable and toxic, and the industrial operability is poor.
The similar technology has poor industrial operability due to the fact that the operation and separation difficulties of the oxidation reaction are not broken through yet, and the technology still stays in a laboratory stage till now and is not expanded or applied industrially.
The invention aims to overcome the defects of the prior art, provides an industrially operable clean production method of sodium chromate, replaces the existing high-temperature oxidizing roasting method of chromite, greatly improves the chromium recovery rate, reduces the discharge amount of high-toxicity chromium slag, solves the pollution problem from the production source and reduces the production cost.
The invention is a phase separation technology of direct cooling crystallization in a high-concentration medium, the concentration of NaOH medium is in high-low one-way reduction, and Cr-Al synchronous crystallization-metastable state countercurrent washing purification, which is completely different from Japanese patent; the invention omits the complicated operation of evaporation concentration and stepwise control, so the method is simple and the industrial operability is greatly improved.
The invention is based on that NaOH is used as a substrate, the traditional sodium carbonate high-temperature (1100 ℃) oxidizing roasting is replaced by gas-liquid-solid three-phase continuous oxidation reaction in a low-temperature molten salt medium (less than 550 ℃), and the total reaction formula is as follows:
the traditional method is a gas-solid reaction of mild sintering:
the new method is easy to control the reaction quantitatively in molten salt medium with good fluidity, and the transfer process is greatly enhanced compared with heterogeneous roasting, so that the oxidation extraction rate of chromium is greatly improved at a lower temperature, and the slag quantity is reduced.
The key problem of thetechnical feasibility of the new reaction method is to solve the problem of large amount of free sodium hydroxide in the molten salt medium (theory)8 times the amount) and NaOH-Na2CrO4-NaAlO2The separation problem of (2). The method adopts a new method of unidirectional separation-metastable phase separation of high-concentration medium and is established on Na+/OH-,CrO4 2-,AlO2 --H2On the basis of comprehensive optimization of O quaternary system phase equilibrium and crystallization-dissolution dynamics, and in combination with engineering operability, an efficient alkali-chromium-aluminum separation effect is obtained.
In the experiment, the invention discovers that the chromium is leached in a high-concentration sodium hydroxide solution area (NaOH 500-.
The metastable phase separation method of the invention discovers that the sodium aluminate presents a supersaturated state (more than the equilibrium solubility is more than 20-30g/l, calculated by simple substance aluminum) in the process of the countercurrent washing of the coarse crystal, so that the aluminum is enriched in the washing liquid and separated from the chromium, thereby replacing the complex process of the step crystallization of chromium and aluminum salt and the decomposition of complex salt proposed by the prior art.
Based on the findings of the above chemical regularity studies, the technical method formed is described in detail as follows:
(1) the reaction system is that chromite is subjected to oxidative decomposition in a liquid phase flowing medium of sodium hydroxide fused salt by using air, the reaction temperature is 500-550 ℃, the sodium hydroxide dosage is 3: 1-6: 1 of alkali and ore (weight ratio), the reaction time is 1-6 hours, and the conversion rate of converting chromium from trivalent chromium into water-soluble hexavalent chromium can reach 99%;
leaching the oxidative decomposition product of the chromite by using water or a chromium residue washing solution to obtain a hexavalent chromium leaching solution with high NaOH concentration; the leaching temperature is 90-150 ℃, the concentration of the leaching solution is 850g/l of NaOH 450-2CrO4With NaAlO2The saturation concentration under the condition is approached;
(2) subjecting the hexavalent chromium leachate to Na treatment2CrO4-NaAlO2Cooling and crystallizing synchronously, wherein the cooling and crystallizing end point temperature is 20-50 ℃, and Na containing 10-20% of free NaOH is obtained2CrO4With NaAlO2Mixed coarse crystal and crystallization mother liquor, the crystallization rate can reach 70 percent;
(3) evaporating and dehydrating the crystallization mother liquor separated by the conventional method, returning the crystallization mother liquor to a molten salt liquid phase chromite oxidation reaction system for recycling, and entering the next washing and purification process of mixed coarse crystals;
(4) for the above Na2CrO4-NaAlO2The mixed coarse crystals are subjected to multistage countercurrent washing, the general stage number is 2-3 stages, water is fed from the last stage, the washing water amount is 0.2-0.5ml/g of coarse crystals, the washing temperature is 40-90 ℃, so that free alkali and sodium aluminate are separated out, and purified sodium chromate crystal products are obtained, namely the products of the method, can be connected with a sodium bichromate processing section of the existing chromium salt industry, and are processed into a series of chromium salt products; the obtained coarse crystal cleaning solution enters the next working procedure.
(5) Adjusting the alkali of the coarse crystal washing liquid obtained in the step (4) to crystallize sodium aluminate, adding sodium hydroxide to adjust the coarse crystal washing liquid until the concentration of the sodium hydroxide reaches 400-600g/l, obtaining coarse crystals of sodium aluminate and crystallization mother liquor at the temperature of 20-50 ℃, and returning the crystallization mother liquor to the sodium chromate crystallization process (3);
(6) washing the coarse crystal of sodium aluminate, removing alkali and chromium, and returning the washing liquid to the sodium aluminate crystallization process (5);
(7) dissolving the sodium aluminate crystals obtained in the step (6) in the presence of Al2O3·3H2Hydrolysis in the presence of O seed crystals to form Al2O3·3H2O product and hydrolysate with crystal seed circulating amount of 30-50% and hydrolysis condition similar to that of Bayer process in alumina industry to separate Al2O3·3H2And (5) after the product O is produced, concentrating the hydrolysis mother liquor and returning to the step (5).
The sodium hydroxide in the system is completely returned and used in principle by the return circulation of the crystallization mother liquor in the steps without acid neutralization and sodium ion loss; the desired reaction time depends on the reaction conditions.
The invention provides an improved method for preparing sodium chromate by liquid-phase oxidation of chromite by sodium hydroxide molten salt, which has incomparable superiority compared with the existing industrial technology-roasting method at home and abroad:
(1) the invention is the combination of high-efficient oxidative decomposition reaction and separation technology, which can improve the recovery rate of chromium by 10-20% compared with the prior art, and the total chromium content of the chromium slag is reduced to less than or equal to 0.5% (10% higher than the foreign advanced calcium-free roasting method and 20% higher than the domestic one-time roasting method);
(2) the chromium slag produced by the method is 600Kg/T product, which is only 1/4 of the roasting method, the total amount of chromium discharged to the environment is reduced to 1/30 of the roasting method, no dust and waste gas are produced, and the pollution is controlled from the production source;
(3) the alkali circulation and separation technology of the invention greatly reduces the energy consumption and the chemical consumption, simplifies the process and the equipment, improves the industrial operability, reduces the energy consumption by 30 percent compared with the prior art, and has no process loss of sodium hydroxide;
(4) the invention has strong operability in industrial implementation and is the first time in the domestic 1000 tons of sodium chromate per year.
FIG. 1 is a process flow diagram of the present invention
Example 1:
and (3) dehydrating the alkali liquor circularly returned to the reaction kettle, heating to 520 ℃, adding 98% of chromite with the particle size of 200 meshes, wherein the weight ratio of the alkali to the chromite is 4: 1, and introducing air to react for 4 hours under the condition of complete mixing to obtain an oxidative decomposition product. Leaching the oxidation decomposition product by using returned chromium slag washing liquid to ensure that the leaching liquid contains 600g/l of NaOH and the temperature is 110 ℃. After leaching for 1 hour, slowly cooling the leaching solution to 25 ℃, and synchronously cooling and crystallizing; filtering to separate Na containing free NaOH 14%2CrO4With NaAlO2Mixed type coarse crystal (mother liquor is stored and used for the next time), the coarse crystal is subjected to 2 times of countercurrent washing at 60 ℃ by using the washing water amount of 0.3ml/g coarse crystal, and the coarse crystal washing liquid is filtered and separated to obtain purified Na2CrO4And (5) producing the product. Adding NaOH to adjust the concentration of NaOH in the coarse crystal washing liquid to 500g/l, aging for 2 hours at 30 ℃ to obtain NaAlO2Coarse crystals and a crystallization mother liquor,adding chromium slag to dissolve NaAlO after filtering2The dissolution solution contains 200g/l of NaOH, and Al with 40% of aluminum content is added into the dissolution solution2O3·3H2Decomposing and aging O crystal seed for 50 hours at 40 ℃ to obtain Al2O3·3H2And filtering and separating mother liquor from the O product and the hydrolysate, and recycling all the mother liquor to the next production. The obtained sodium chromate product contains 27 percent of chromium (calculated by simple substance chromium), 1.0 percent of NaOH, 0.4 percent of Al and 0.3 percent of Fe (calculated by even simple substance), and the impurity content is lower than that of the sodium chromate alkaline solution of the roasting method.
Example 2:
the alkali liquor circularly returned to the reaction kettle is dehydrated and heated to 520 ℃, 98 percent of chromite with the grain diameter of 200 meshes is added,the weight ratio of alkali to ore is 4: 1, and air is introduced to react for 4 hours under the condition of complete mixing, so as to obtain the oxidative decomposition product. Leaching the oxidation decomposition product by using returned chromium slag washing liquid to ensure that the leaching liquid contains 680 g/l of NaOH and the temperature is 115 ℃. After leaching for 1 hour, slowly cooling the leaching solution to 30 ℃, synchronously cooling and crystallizing, and filtering and separating Na containing 15 percent of NaOH2CrO4With NaAlO2Mixed type coarse crystal (mother liquor is stored and used for the next time), the coarse crystal is subjected to 2 times of countercurrent washing at 70 ℃ by using the washing water amount of 0.3ml/g coarse crystal, and the coarse crystal washing liquid is filtered and separated to obtain purified Na2CrO4And (5) producing the product. NaOH is added to adjust the NaOH concentration of the coarse crystal washing liquid to 570g/l, and the coarse crystal washing liquid is aged for 2 hours at 40 ℃ to obtain NaAlO2Filtering the coarse crystal and the crystallization mother liquor, adding chromium slag to dissolve NaAlO2The dissolution solution contains 200g/l of NaOH, and Al with 40% of aluminum content is added into the dissolution solution2O3·3H2Decomposing and aging O crystal seed for 50 hours at 40 ℃ to obtain Al2O3·3H2And filtering and separating mother liquor from the O product and the hydrolysate, and recycling all the mother liquor to the next production. The obtained sodium chromate product contains 26.8 percent of chromium (calculated by simple substance chromium), 1.1 percent of NaOH, 0.4 percent of Al and 0.3 percent of Fe (calculated by uniform substance), and the impurity content is lower than that of the sodium chromate alkaline solution of the roasting method.
Example 3:
the alkali liquor circularly returned to the reaction kettle is dehydrated and heated to 520 ℃, 98 percent of chromite with the grain diameter of 200 meshes is added, and the alkali and the ore are mixedThe weight ratio is 4: 1, air is introduced to react for 4 hours under the condition of complete mixing, and the oxidative decomposition product is obtained. Leaching the oxidation decomposition product by using returned chromium slag washing liquid to ensure that the leaching liquid contains 800g/l of NaOH and the temperature is 125 ℃. After leaching for 1 hour, slowly cooling the leaching solution to 50 ℃, carrying out synchronous cooling crystallization, and filtering to separate Na containing 19 percent of NaOH2CrO4With NaAlO2Mixed type coarse crystals (mother liquor is stored and used next time), and the coarse crystals are subjected to 3 times of countercurrent washing at 90 ℃ by using the washing water amount of 0.5ml/g of coarse crystals. Filtering and separating out coarse crystal washing liquid to obtain purified Na2CrO4And (5) producing the product. NaOH is added to adjust the NaOH concentration of the coarse-grained washing liquid to 450g/l, and the coarse-grained washing liquid is aged for 2 hours at the temperature of 30 ℃ to obtain NaAlO2Filtering the coarse crystal and the crystallization mother liquor, adding chromium slag to dissolve NaAlO2The dissolution solution contains 200g/l of NaOH, and Al with 40% of aluminum content is added into the dissolution solution2O3·3H2Decomposing and aging O crystal seed for 50 hours at 40 ℃ to obtain Al2O3·3H2And filtering and separating mother liquor from the O product and the hydrolysate, and recycling all the mother liquor to the next production. The obtained sodium chromate product contains 25 percent of chromium (calculated by simple substance chromium), 1.5 percent of NaOH, 0.5 percent of Al and 0.4 percent of Fe (calculated by even simple substance), and the impurity content is lower than that of the sodium chromatealkaline solution of the roasting method.

Claims (5)

1. A clean production method of sodium chromate is characterized in that a reaction system is to carry out oxidative decomposition on chromite in a liquid phase flow medium of sodium hydroxide molten salt, and sodium chromate is prepared from a hexavalent chromium leaching solution containing alkali obtained after water leaching, and the method comprises the following steps:
(1) heating and leaching the oxidation decomposition product of the chromite by using water or a chromium residue washing solution to obtain a hexavalent chromium leaching solution with high NaOH concentration;
(2) na is carried out on hexavalent chromium leaching solution2CrO4-NaAlO2Cooling and crystallizing synchronously to obtain Na containing free NaOH2CrO4-NaAlO2Mixed coarse crystal and crystallization mother liquor;
(3) evaporating and dehydrating the crystallized mother liquor, and returning the crystallized mother liquor to a molten salt liquid-phase oxidation decomposition chromite reaction system;
(4) for the above Na2CrO4-NaAlO2The mixed coarse crystals are subjected to multi-stage countercurrent washing to separate free alkali and sodium aluminate to obtain purified Na2CrO4Crystallizing the product and a coarse crystal washing liquid, and enabling the obtained coarse crystal washing liquid to enter the step (5);
(5) adjusting the alkali of the coarse crystal washing liquid obtained in the step (4) to crystallize sodium aluminate to obtain NaAlO2Coarse crystal and crystallization mother liquor, and the crystallization mother liquor is returned to Na2CrO4A crystallization step (3);
(6) for NaAlO2Washing the coarse crystal, removing alkali and chromium, and returning the washing liquid to NaAlO2A crystallization step (5);
(7) NaAlO obtained in the step (6)2Crystals dissolved in Al2O3·3H2Hydrolysis in the presence of O seed crystals to form Al2O3·3H2O products and hydrolysate.
2. The clean production method of sodium chromate as set forth in claim 1, wherein the leaching temperature of the oxidative decomposition products of chromite is 90-150 ℃, and the NaOH concentration of the leachate is 850 g/l.
3. The process for the clean production of sodium chromate as claimed in claim 1, wherein the leachate is subjected to Na2CrO4-NaAlO2Synchronously cooling and crystallizing, wherein the cooling crystallization end point temperature is 20-50 ℃.
4. The process for the clean production of sodium chromate as claimed in claim 1, wherein the Na is added2CrO4-NaAlO2And (3) carrying out multistage countercurrent washing on the mixed coarse crystals, wherein the stages are 2-3 stages, the washing temperature is 40-90 ℃, and the washing water amount is 0.2-0.5ml/g of coarse crystals.
5. The clean production method of sodium chromate as claimed in claim 1, wherein the concentration of NaOH in the alkali-adjusting crystallization in step (5) is 400-600g/l, and the temperature of the alkali-adjusting crystallization is 20-50 ℃.
CN98100556A 1998-02-20 1998-02-20 Clean production of sodium chlomate Expired - Lifetime CN1062528C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN98100556A CN1062528C (en) 1998-02-20 1998-02-20 Clean production of sodium chlomate

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN98100556A CN1062528C (en) 1998-02-20 1998-02-20 Clean production of sodium chlomate

Publications (2)

Publication Number Publication Date
CN1226512A CN1226512A (en) 1999-08-25
CN1062528C true CN1062528C (en) 2001-02-28

Family

ID=5216095

Family Applications (1)

Application Number Title Priority Date Filing Date
CN98100556A Expired - Lifetime CN1062528C (en) 1998-02-20 1998-02-20 Clean production of sodium chlomate

Country Status (1)

Country Link
CN (1) CN1062528C (en)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7968066B2 (en) 2003-03-19 2011-06-28 Institute Of Process Engineering Chinese Academy Of Sciences Method for production of alkali metal chromates
CN101659444B (en) * 2008-08-27 2012-07-25 中国科学院过程工程研究所 Clean production method for preparing sodium chromate from chromite
CN102127654B (en) * 2010-01-13 2013-01-23 中国科学院过程工程研究所 Method for decomposing chromium-containing vanadium slag by using sodium hydroxide molten salt
CN102424422B (en) * 2011-09-09 2013-08-07 甘肃锦世化工有限责任公司 Method for removing aluminum by neutralizing sodium chromate alkali solution
CN104512929B (en) * 2013-09-30 2016-03-30 湖北振华化学股份有限公司 A kind of method being separated caustic alkali and chromic salt in the solid mixture containing caustic alkali and chromic salt
CN104480313B (en) * 2014-12-04 2017-12-22 北京科技大学 A kind of method of vanadium and chromium in extraction solid
CN110093496A (en) * 2019-05-10 2019-08-06 四川久远环境技术有限公司 A kind of ferrochrome dust resourcesization containing chromium powder utilize method

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1153142A (en) * 1995-12-27 1997-07-02 冶金工业部长沙矿冶研究院 Method for preparation of sodium chromate chamotte
RU2096332C1 (en) * 1995-11-28 1997-11-20 Арон Михайлович Халемский Method and furnace for processing chromite ore into sodium chromate

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2096332C1 (en) * 1995-11-28 1997-11-20 Арон Михайлович Халемский Method and furnace for processing chromite ore into sodium chromate
CN1153142A (en) * 1995-12-27 1997-07-02 冶金工业部长沙矿冶研究院 Method for preparation of sodium chromate chamotte

Also Published As

Publication number Publication date
CN1226512A (en) 1999-08-25

Similar Documents

Publication Publication Date Title
US4224287A (en) Process for the preparation of pure aluminum oxide
CN1827527A (en) Process for preparing lithium chlorate by lithium extracted from lepidolite
CN102515220B (en) Method for extracting alumina and gallium oxide from pulverized fuel ash to prepare aluminum oxide nanometer and polymeric ferric silicate sulfate
CN101058852A (en) Multistage counter current acid leaching process containing nickel serpentine ore
CN107892317B (en) Method for recovering vanadium in calcified vanadium precipitation tailings and preparing nano calcium carbonate
CN1062528C (en) Clean production of sodium chlomate
CN1162330C (en) Clean production method of potassium chromate
CN106629847A (en) Method for preparing vanadium trioxide from sodium-vanadate salt
CN103663505A (en) Method for treating potassium feldspar according to sub-molten salt method to prepare potassium carbonate
CN1760117A (en) Method for recovering vitriol from waste vitrol containing metal salt
CN101880772A (en) Method for recycling magnesium from magnesium-containing waste solution
CN111139356A (en) Method for extracting lithium from lithium-containing low-magnesium brine
Pang et al. Chemical dehydration coupling multi-effect evaporation to treat waste sulfuric acid in titanium dioxide production process
CN1317185C (en) Preparation process for purifying graphite by liquid phase method
CN1103321C (en) Clean production process of ammonium chromate crystal
CN1683247A (en) Process for producing anhydrous aluminium chloride
CN1337360A (en) Method of preparing cobelt chloride with colbalt slag containing Fe and Mg
CN102092753B (en) Alcoholization removing method of impurity iron in aluminum sulfate solution
CN1106358A (en) Method for extracting lithium salt from brine
CN1064931C (en) Solvent process for preparing strontium carbonate
CN1014318B (en) Recovering ga from production of alumina with dissolving method
CN1830797A (en) Method and technology of producing precipitated barium sulphate using white carbon black waste liquor
CN1072656A (en) The production method of aluminium hydroxide
CN109824068B (en) Extraction of Rb from Low-concentration brine+And method for producing highly pure rubidium salt
CN110983059B (en) Method for recovering copper and arsenic from copper smelting white smoke leachate and arsenic filter cake

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
CX01 Expiry of patent term
CX01 Expiry of patent term

Granted publication date: 20010228