CN106395759A - A method of producing high-purity sodium sulfide - Google Patents
A method of producing high-purity sodium sulfide Download PDFInfo
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- CN106395759A CN106395759A CN201610510696.1A CN201610510696A CN106395759A CN 106395759 A CN106395759 A CN 106395759A CN 201610510696 A CN201610510696 A CN 201610510696A CN 106395759 A CN106395759 A CN 106395759A
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- sodium sulfide
- filtrate
- purity
- sodium
- leaching liquid
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
- C01B17/24—Preparation by reduction
- C01B17/26—Preparation by reduction with carbon
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
- C01B17/36—Purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Abstract
A method of producing high-purity sodium sulfide is disclosed. The method includes S100) a step of adding raw coal, mirabilite and a catalyst that is ferric oxide into a ball mill, and grinding, with the weight ratio of the mirabilite, the raw coal and the ferric oxide being 5:2:0.04, S200) a step of, after grinding, conveying into a stirrer, and stirring to fully mix the mixture, and S300) a step of, after stirring is finished, spraying the mixture into a calciner, maintaining a slightly-negative pressure atmosphere in the calciner, controlling the air excessive amount during calcination through a flue residual-oxygen detecting device, and maintaining the calcination temperature to be 1000-1100 DEG C through a material temperature monitoring device and a flue gas temperature monitoring device. The sodium sulfide produced by the method is high in purity and wide in application.
Description
Technical field
The invention belongs to chemical field, particularly to a kind of high-purity sulfuration production method of sodium.
Background technology
Sodium sulfide is also known as smelly alkali, smelly soda, yellow alkali, akali sulphide.Sodium sulfide is inorganic compound, bright sulfur
Sodium is colorless crystalline powder；Moisture absorption is strong, soluble in water；Aqueous solution is in that strong basicity is reacted；Touch skin and
Can cause during hair to burn；Therefore sodium sulfide is commonly called as akali sulphide.At present, China's industrial sodium sulfide production method master
There are two kinds, one kind is main product method Natrii Sulfas calcination method；One kind is to pay product method blanc fixe to pay product sulfuration
Sodium.Existing Natrii Sulfas are mixed with coal dust and are only simply mixed, and Natrii Sulfas are usually irregular lamellar or granule,
It is simply mixed, its contact area is little, therefore, during heating reduction, easily cause Natrii Sulfas, coal dust reacts imperfect,
Coal dust calcining not exclusively, produces substantial amounts of waste gas, and leads to the sodium sulfide producing to yield poorly.Both the above is given birth to
The industrial sodium sulfide producing has the problem that impurity is many, iron content is high, can be to final products matter in application process
Amount brings impact, and such as high-sulfurized for iron content sodium products application and copper ore dressing industry, producing copper products will
The impure problem of quality occurs.As high-sulfurized for iron content sodium products application, in leather industry, client produces
Leather products arise that the bad quality problems of color.Therefore, the content removal reducing sodium sulfide product iron has
Evil impurity, can produce good effect to products application.Currently, in China's sodium sulfide product, iron content typically exists
300-600ppm.The price of anhydrous sodium sulfide is the several times of aqueous sodium sulfide it is therefore necessary to sodium sulfide
Drying makes further research.
Content of the invention
For the defect of prior art, the invention provides a kind of high-purity sulfuration production method of sodium.
A kind of high purity sodium sulfide production method, comprises the steps：S100：By raw coal, Natrii Sulfas, catalysis
Agent iron sesquioxide is positioned over ball mill grinding, wherein Natrii Sulfas：Coal：Iron sesquioxide is：5：2：0.04
(weight ratio)；S200：Agitator mix and blend is sent into so as to mix homogeneously after grinding；S300：Stirring
After the completion of, mixture is sprayed in calcining furnace, maintains tiny structure atmosphere in calcining furnace, examined by the residual oxygen of flue
Survey device, control calcining air excess amount, by temperature of charge supervising device and flue-gas temperature supervising device,
Calcining heat is made to maintain 1,000 1100 DEG C；The sodium sulfide that calcining generates is discharged from fluid bed bottom discharge
To alkali base；Alkali base becomes liquid through thermal melting, with water, alkali base is washed into sodium sulfide content and is more than 300 g/l
Solution, standing purifies clarification, obtains reductive leaching liquid；S400：Sodium carbonate, hydrogen-oxygen is added in leaching liquid
Change sodium, Alumen is to remove the calcium in leaching liquid, magnesium plasma and the heavy metal such as ferrum, arsenic, lead, cadmium, antimony
Ion is so as to total content in Natrii Sulfas carbon reductive leaching liquid for the metal ion such as arsenic, lead, cadmium, antimony is less than 10ppm
Filtrate；Filtrate is pumped into crystallization tank, through the crystallization of vacuum quick freezing, centrifuge dehydration.
Optionally, also comprise the steps：S500：Manganese powder and/or manganio is added in solution of zinc sulfate
Alloyed powder, temperature is 50 DEG C and pH ＞ 4.0, stirring reaction, after the completion of reaction, filtration separation, afterwards
Through evaporating, concentrating and crystallizing, obtain high-purity sulfuric acid zinc, the high-purity sulfuric acid zinc of preparation is added by every cube of filtrate
Enter 5-10 kilogram of amount of zinc sulfate and weigh zinc sulfate, every cube of filtrate 1 cube of solution of zinc sulfate of corresponding preparation；Press
Add barium sulfide 150kg in every cube of water, take clear liquid standby；The solution that both the above is prepared, is simultaneously introduced
In sodium sulfide filtrate, stirring, 80 revs/min of mixing speed, reaction temperature controls more than 80 DEG C, then
Precipitate 12 16 hours, after remove impurity clarification, send evaporization process, obtain high purity sodium sulfide through evaporation and concentration.
Optionally, also comprise the steps：S600：A certain amount of crystalline sodium sulfide raw material is taken to be placed in vacuum rake type
In drying machine, hermetically drying machine, open vacuum pump, open roots blower. after treating vacuum meter stably, open
Open oil circulating pump, and begin to warm up recycle oil, control the temperature of recycle oil, rake type drier at the uniform velocity stirs. set
After received shipment row certain time, stop stirring, close drying machine upper valve, into drying machine, be passed through nitrogen,
Open dog-house, rapid feeding, survey its residual water content using thermogravimetric analyzer. reaction to be drained off is all tied
Shu Hou, closes vacuum pump and roots blower, stops stirring, cooling discharge；Wherein vacuum necessary >=0.096
MPa, is dried using two sections of temperature, and 85 DEG C of one section of low temperature carries out heating 1h；115 DEG C of two-stage nitration high temperature
Carry out heating 0.5h；Material is cooled to 40 DEG C with bottom discharge.
The invention has the beneficial effects as follows：Natrii Sulfas and the contact area of coal dust is made to become big by grinding, plus
During thermal reduction, reaction is more abundant, improves sodium sulfide yield；By calcining the control of negative pressure and temperature, no
The content of product soluble impurity only can be reduced, improve feed stock conversion, lower consumption, play energy-saving
Effect, calcine the SO of generation simultaneously2Content is greatly reduced, and alleviates the burden of environmental protection；By adding carbon
Sour sodium, sodium hydroxide can more effectively process except the calcium in Natrii Sulfas carbon reductive leaching liquid, magnesium, arsenic, lead,
The impurity metal ions such as cadmium, antimony；Using high-purity sulfuric acid zinc and barium sulfide solution, can remove in sodium sulfide
Iron ion so that iron ion content substantially reduces (less than 3ppm)；Control in dry run and vacuum is dried
The conditions such as degree, baking temperature, drying time, drop temperature solving that crystalline sodium sulfide is oxidizable, cohere
Problem, thus obtain highly purified anhydrous sodium sulfide.
Specific embodiment
Understandable for enabling the above objects, features and advantages of the present invention to become apparent from, below to the present invention's
Specific embodiment is described in detail, and the above and other purpose, feature and the advantage that make the present invention will more
Clearly.
Embodiment 1
The present embodiment introduces the production method of high purity sodium sulfide, and it comprises the steps：
S100：Raw coal, Natrii Sulfas, catalyst iron sesquioxide are positioned in ball mill, are ground to 120～130
Mesh.Wherein Natrii Sulfas：Coal：Iron sesquioxide is：5：2：0.04 (weight ratio).
S200：Agitator mix and blend is sent into after grinding.So that coal dust and Natrii Sulfas after pulverizing after grinding
Contact area increases, thus improving the completeness of reaction.Coal dust mirabilite powder stirring after pulverizing is so as to mix
Close uniformly, so that being fully contacted of mirabilite powder and coal dust, improve and react completeness.
S300：After the completion of stirring, mixture is sprayed in calcining furnace, calcining under 900 1100 DEG C of high temperature is gone back
Former.Impurity in industrial sodium sulfide product is Na2CO3、Na2Sx、Na2SO3、Na2S2O3、Fe2-, water-insoluble
Deng.Wherein Na2CO3、Na2SxMainly produce in converter calcination process, therefore control calcine technology,
The content of its impurity can be substantially reduced.In calcination process, Na2CO3、Na2SxThe main cause being formed：1)
System negative pressure is not enough, CO in kiln2Discharge is not in time：Na2S+4CO2=Na2CO3+SO2+3CO；2) calcine air capacity
Surplus, oxygen is had more than needed：2Na2S+1/2O2=Na2O+Na2S2(sodium polysulphide) is directed to above-mentioned reason, system of the present invention
Fixed following prioritization scheme：1) tiny structure atmosphere in control kiln, the CO that reaction produces2、SO2Drawing in time (can
Reduce SO2Generation), it is to avoid the Na of generation2S participates in side reaction；2) add flue residual oxygen detection means, sternly
Control calcining air excess amount, controls Na2S2Generation；3) monitoring of temperature of charge and flue-gas temperature in kiln are set up
Monitoring, grasps calcination reaction terminal and discharging time, prevents burning or underburnt, and shortening " grey black " is come out of the stove cold
But the time；4) when adopting long converter site base technique, also need thermosol alkali mist is drawn in time and absorbed, prevent
Sealing vapour enters kiln and produces Na2CO3.By several measures above, not only can reduce product soluble impurity content,
Improve feed stock conversion, lower consumption, play energy-saving effect, calcine the SO of generation simultaneously2Content
Substantially reduce, alleviate the burden of environmental protection.
The sodium sulfide that calcining generates is discharged from fluid bed bottom discharge and is obtained alkali base；Alkali base becomes liquid through thermal melting,
With water, alkali base is washed into the solution that sodium sulfide content is more than 300 g/l, standing purifies clarification, reduced
Leaching liquid.
S400：Add sodium carbonate, sodium hydroxide in leaching liquid, Alumen is to remove Natrii Sulfas carbon reductive leaching liquid
In calcium, magnesium plasma and the heavy metal ion such as ferrum, arsenic, lead, cadmium, antimony be so as to arsenic, lead, cadmium, antimony
It is less than 10ppm Deng total content in Natrii Sulfas carbon reductive leaching liquid for the metal ion；
Cubage according to recording calcium ions and magnesium ions in leaching liquid adds the amount of sodium carbonate, simultaneously excessive 20-30%；
And add according to recording the heavy metal ion contents such as arsenic, lead, cadmium, antimony in former Natrii Sulfas carbon reductive leaching liquid and calculating
The amount of sodium sulfide, excessive 30-40%；Being subsequently adding sodium hydroxide makes the pH value of Natrii Sulfas carbon reductive leaching liquid reach
9-11；Adding 0.2-0.6%wt Alumen makes the various deposit sedimentations of generation, is eventually adding sulphuric acid and adjusts
The pH value of Natrii Sulfas carbon reductive leaching liquid reaches 6.6-7.2；
Former Natrii Sulfas carbon reductive leaching liquid pump after polishing purification is entered crystallization tank, crystallizes through vacuum quick freezing,
Pump into standing separation groove standing 30-60min, first isolate clear liquid, subsequently into centrifuge dehydration operation.Using
On the one hand present invention process control condition, can reduce Energy in use on the premise of product purity height.
Experimental example 1
Containing Sulfur na concn is 34.1% Natrii Sulfas carbon reductive leaching liquid, adds 3100g/m3Sodium carbonate and 900
g/m3Sodium sulfide, being subsequently adding sodium hydroxide makes the pH value of Natrii Sulfas carbon reductive leaching liquid reach 10；Add
0.35%wt poly-ferric chloride makes the various deposit sedimentations of generation, is eventually adding sulphuric acid and adjusts the reduction of Natrii Sulfas carbon
The pH value of leaching liquid reaches 7.2, so processes through polishing purification and obtains the extremely low Natrii Sulfas of various impurity contents
Carbon reductive leaching liquid, inputs Natrii Sulfas carbon reductive leaching liquid storage tank, then by pumping into the crystallizer 70min time
Vacuum quick freezing crystallizes 30 DEG C of technological temperature, and vacuum degree control, in -0.096Mp, inputs standing separation dress
Put standing 35min, then centrifuge carries out solid-liquid separation, mother solution inputs mother liquor holding tank, and crystal enters storage tank.
Experimental example 2
Containing Sulfur na concn is 29.8% Natrii Sulfas carbon reductive leaching liquid, adds 2900g/m3Sodium carbonate and 980.3
g/m3Sodium sulfide, being subsequently adding sodium hydroxide makes the pH value of Natrii Sulfas carbon reductive leaching liquid reach 10；Add
0.45%wt poly-ferric chloride makes the various deposit sedimentations of generation, is eventually adding sulphuric acid and adjusts the reduction of Natrii Sulfas carbon
The pH value of leaching liquid reaches 6.8, so processes through polishing purification and obtains the extremely low Natrii Sulfas of various impurity contents
Carbon reductive leaching liquid, input Natrii Sulfas carbon reductive leaching liquid storage tank, then by pump into crystallizer 80min when
Between vacuum quick freezing crystallize 60 DEG C of technological temperature, vacuum degree control in -0.089Mpa, inputs standing separation
Device stands 40min, then centrifuge carries out solid-liquid separation, and mother solution inputs mother liquor holding tank, and crystal enters storage tank.
In order to further remove iron ion, adding sodium carbonate, sodium hydroxide, Alumen filters and precipitates
To after filtrate, can also comprise the steps：
S500：Prepare solution of zinc sulfate.The impurity such as more copper, cadmium, nickel, cobalt are contained in industrial sulphuric acid zinc
Element, if directly adopting industrial sulphuric acid zinc, can introduce impurity in the preparation of sodium sulfide.For this present invention,
Add manganese powder and/or manganese-base alloy powder in solution of zinc sulfate, temperature is 50 DEG C and pH ＞ 4.0, stirs
Mix reaction, after the completion of reaction, filtration separation, you can so that the copper in industrial sulphuric acid zinc, cadmium, nickel and cobalt is first
Element remove, after through evaporating, concentrating and crystallizing, that is, obtain high-purity sulfuric acid zinc.The reduction potential of manganese metal is higher than
The reduction potential of metallic zinc, this makes manganese metal be better than metallic zinc to the diadochy of copper, cadmium, cobalt and nickel；
At a lower temperature, you can realize the deep purifying of copper, cadmium, cobalt and nickel, thoroughly change existing zinc powder net
In metallization processes, for removing copper cadmium nickel cobalt and avoiding returning of copper cadmium molten, solution need to be carried out rise gentle cooling behaviour
The present situation made.Additionally, the higher reduction potential of manganese metal so that in purification slag copper, cadmium, cobalt, nickel stable
Property is preferable, it is to avoid return the generation of molten phenomenon.
Experimental example 3
Measure 1.6L and remove solution of zinc sulfate (Zn after ferrum:140g/L, Cu:310mg/L, Cd:502mg/L,
Ni:14.6mg/L, Co:12.8mg/L, pH=4.9), open and stir and be heated to 50 DEG C, subsequently press
5 times of addition manganin powder (Mn according to copper and cadmium gross mass:98%) terminate after insulation reaction 120min anti-
Should, vacuum filtration simultaneously collects filtrate and filtering residue.Copper in gained filtrate, cadmium, cobalt, nickel concentration be respectively 0.16,
0.13rd, 0.22,0.14mg/L, removal efficiency, all more than 98%, meets impurity removal requirement.
The high-purity sulfuric acid zinc of preparation is added 5-10 kilogram of amount of zinc sulfate to weigh zinc sulfate by every cube of filtrate,
Every cube of filtrate 1 cube of solution of zinc sulfate of corresponding preparation.
Formulating vulcanization barium solution, adds barium sulfide 150kg by every cube of water, barium sulfide (BaS) is dissolved
15Be, 90 DEG C of water temperature, precipitates 70 minutes, takes clear liquid standby, every cube of filtrate need to add 0.06-0.08 to stand
The barium sulfide solution of side；The solution that both the above is prepared, is simultaneously introduced in sodium sulfide filtrate, stirring, stirs
Mix 80 revs/min of speed, reaction temperature controls more than 80 DEG C, then precipitate 12 16 hours, remove impurity is clear
In sodium sulfide solution after clear, iron ion content, in 3-8PPM, then send evaporization process；Through evaporation and concentration, system
Piece is packed, i.e. high purity sodium sulfide.
Embodiment 2
The present embodiment introduces the drying meanss for the high purity sodium sulfide prepared by embodiment 1.Industry
The main component of product sodium sulfide is Na2S·9H2O and Na2S·5.5H2O, in order to obtain anhydrous sodium sulfide, needs
Process is dried to it.
Specifically, S600：A certain amount of crystalline sodium sulfide raw material is taken to be placed in vacuum rake dryer, sealing is dry
Dry machine, opens vacuum pump, when vacuum reaches -0.08MPa in machine to be dried, opens roots blower. treat
Vacuum meter stably after, ON cycle oil pump, and begin to warm up recycle oil, control the temperature of recycle oil, rake
Formula drying machine at the uniform velocity stirs. and after equipment runs certain time, stop stirring, close drying machine upper valve,
It is passed through nitrogen into drying machine, open dog-house, rapid feeding, survey its remaining water using thermogravimetric analyzer and contain
Amount. after reaction to be drained off all terminates, close vacuum pump and roots blower, stop stirring, cooling discharge.
Sodium sulfide crystal to be made occurs without melting and viscous wall in process of vacuum drying, and vacuum is necessary >=0.096MPa,
This is the key that can crystal sodium sulfide be dried production, can also effectively stop the oxygen of sodium sulfide simultaneously
Change variable color.It is dried using two sections of temperature, 85 DEG C of one section of low temperature carries out heating 1h, it is to avoid fusing simultaneously；
115 DEG C of two-stage nitration high temperature carries out heating 0.5h, is mainly to ensure that and is dried completely and shortens drying time.It is anti-
After the completion of being only dried, the combustion oxidation of material is it is necessary to be cooled to less than 40 DEG C by material under keeping vacuum condition
Can discharging.
Elaborate a lot of details in order to fully understand the present invention in the above description.But more than retouch
Stating is only presently preferred embodiments of the present invention, and the present invention can be to be much different from other side described here
Implementing, therefore the present invention is not embodied as being limited formula by disclosed above.Simultaneously any it is familiar with this area
Technical staff is without departing from method and the skill that the disclosure above under technical solution of the present invention ambit, can be utilized
Art content makes many possible variations and modification to technical solution of the present invention, or be revised as equivalent variations etc.
Effect embodiment.Every content without departing from technical solution of the present invention, according to the present invention technical spirit to more than
Any simple modification, equivalent variations and modification that embodiment is made, all still fall within technical solution of the present invention protection
In the range of.
Claims (1)
1. a kind of high purity sodium sulfide production method is it is characterised in that comprise the steps：
S100：Raw coal, Natrii Sulfas, catalyst iron sesquioxide are positioned over ball mill grinding, wherein Natrii Sulfas：
Coal：Iron sesquioxide is：5：2：0.04 (weight ratio)；
S200：Agitator mix and blend is sent into so as to mix homogeneously after grinding；
S300：After the completion of stirring, mixture is sprayed in calcining furnace, maintains tiny structure atmosphere in calcining furnace,
By flue residual oxygen detection means, control calcining air excess amount, by temperature of charge supervising device and flue gas
Device for monitoring temperature is so that calcining heat maintains 1,000 1100 DEG C；The sodium sulfide that calcining generates is from fluidisation
Bed bottom discharge is discharged and is obtained alkali base；Alkali base becomes liquid through thermal melting, with water, alkali base is washed into sodium sulfide content
Solution more than 300 g/l, standing purifies clarification, obtains reductive leaching liquid；
S400：Add sodium carbonate, sodium hydroxide in leaching liquid, Alumen is to remove the calcium in leaching liquid, magnesium
The heavy metal ion such as plasma and ferrum, arsenic, lead, cadmium, antimony is so as to the metal ion such as arsenic, lead, cadmium, antimony
Total content in Natrii Sulfas carbon reductive leaching liquid is less than the filtrate of 10ppm；Filtrate is pumped into crystallization tank, passes through
Vacuum quick freezing crystallizes, centrifuge dehydration；
S500：Add manganese powder and/or manganese-base alloy powder in solution of zinc sulfate, temperature be 50 DEG C and
PH ＞ 4.0, stirring reaction, after the completion of reaction, filtration separation, after through evaporating, concentrating and crystallizing, obtain high-purity
Degree zinc sulfate, the high-purity sulfuric acid zinc of preparation is added 5-10 kilogram of amount of zinc sulfate to weigh sulfur by every cube of filtrate
Sour zinc, every cube of filtrate 1 cube of solution of zinc sulfate of corresponding preparation；Add barium sulfide 150kg by every cube of water,
Take clear liquid standby；The solution that both the above is prepared, is simultaneously introduced in sodium sulfide filtrate, stirring, reaction temperature
Degree controls more than 80 DEG C, precipitation, after remove impurity clarification, send evaporization process, obtains through evaporation and concentration high-purity
Degree sodium sulfide.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109704290A (en) * | 2019-03-06 | 2019-05-03 | 铜陵铜冠神虹化工有限责任公司 | A kind of method of purification of crystal akali sulphide |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1244493A (en) * | 1999-09-13 | 2000-02-16 | 甘肃亚盛盐化工业集团有限责任公司 | Production technology of yellow flaky sodium sulfide with low carbon and iron contents |
| CN1850587A (en) * | 2006-05-16 | 2006-10-25 | 内蒙古工业大学 | Method for preparing low-iror anhydrous sodium sulfide by one-step reduction of Glauber salt from coke oven gas |
| CN101602514A (en) * | 2008-06-10 | 2009-12-16 | 四川川眉特种芒硝有限公司 | A kind of manufacture method of special mirabilite with high purity |
| CN105714116A (en) * | 2016-03-16 | 2016-06-29 | 中南大学 | Method for removing copper, cadmium, nickel and cobalt out of zinc sulfate solution through one step |
-
2016
- 2016-07-01 CN CN201610510696.1A patent/CN106395759A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1244493A (en) * | 1999-09-13 | 2000-02-16 | 甘肃亚盛盐化工业集团有限责任公司 | Production technology of yellow flaky sodium sulfide with low carbon and iron contents |
| CN1850587A (en) * | 2006-05-16 | 2006-10-25 | 内蒙古工业大学 | Method for preparing low-iror anhydrous sodium sulfide by one-step reduction of Glauber salt from coke oven gas |
| CN101602514A (en) * | 2008-06-10 | 2009-12-16 | 四川川眉特种芒硝有限公司 | A kind of manufacture method of special mirabilite with high purity |
| CN105714116A (en) * | 2016-03-16 | 2016-06-29 | 中南大学 | Method for removing copper, cadmium, nickel and cobalt out of zinc sulfate solution through one step |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109704290A (en) * | 2019-03-06 | 2019-05-03 | 铜陵铜冠神虹化工有限责任公司 | A kind of method of purification of crystal akali sulphide |
| CN109704290B (en) * | 2019-03-06 | 2022-07-26 | 铜陵铜冠神虹化工有限责任公司 | Purification method of crystalline sodium sulfide |
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