CN107892313A - Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum - Google Patents
Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum Download PDFInfo
- Publication number
- CN107892313A CN107892313A CN201711493077.7A CN201711493077A CN107892313A CN 107892313 A CN107892313 A CN 107892313A CN 201711493077 A CN201711493077 A CN 201711493077A CN 107892313 A CN107892313 A CN 107892313A
- Authority
- CN
- China
- Prior art keywords
- demagging
- brine
- dihydrate gypsum
- reactor
- buffer barrel
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
- C01D3/16—Purification by precipitation or adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
Abstract
The present invention relates to brine rectification process, specifically the process units method of saltcake refined brine and by-product dihydrate gypsum.Demagging reactor is connected by pipeline with baffling groove I, and calcium-removing reactor is connected with baffling groove II and dihydrate gypsum slurry buffer barrel respectively by pipeline, and deliming settling tank is connected with primary brine buffer barrel and dihydrate gypsum slurry buffer barrel respectively by pipeline.Crude brine is added into demagging reactor, according to the amount of magnesium ion in the crude brine for entering demagging reactor, the salt mud that bottom of the barrel and the outflow of demagging reactor bottom are clarified from demagging enters a salt slurry buffer barrel, demagging crude brine from demagging crude brine buffer barrel is pumped into calcium-removing reactor through demagging crude brine, the low calcium clear liquid that the top overflow of deliming settling tank goes out flow to primary brine buffer barrel certainly as primary brine, dihydrate gypsum material pulp pumping is to filter, washed through separation of solid and liquid, output dihydrate gypsum product.By-product dihydrate gypsum realizes the further minimizing of salt refining byproduct in process salt slurry.
Description
Technical field
The present invention relates to the technique of salt refining, specifically a kind of life using saltcake refined brine and by-product dihydrate gypsum
Produce device and production method.
Background technology
During ammonia-soda process soda manufacture, solid crude salt need to be dissolved using fresh water, and remove Ca therein2+、Mg2 +, it is prepared into refined brine.Using traditional " lime-soda method " brine rectification process, it is necessary to consume a large amount of ash breasts, soda ash, cost
It is high, and the salt slurry of a large amount of calcium carbonates of by-product, magnesium hydroxide and dihydrate gypsum.Disposal in industry to salt slurry is substantially salt
Mud carries out being squeezed into cake into filter press, and extruding water outlet enters back into salt dissolving system and prepares a crude brine, filter cake stockpiling processing.
Patent No. 201210517699.X, title：The method for preparing refined brine and its byproduct；Disclose one kind " three times
The method of refined, secondary salt dissolving, a step denitration " refined brine, this method can realize that calcium carbonate is miscellaneous with other in by-product salt slurry
The separation of matter, produce high-quality calcium carbonate product using abandoned salty mud, realize solid waste reducing, be concentrated seawater,
Bitter salt dissolving is refined to provide technical support.But still suffer from that grey breast, soda ash consumption are big, and cost is high to ask using the technology
Topic, and by-product salt slurry amount abatement is limited.
The patent No. 201410147395.8, title：Brine rectification process；Disclose a kind of " lime-saltcake-soda ash " salt
Water refining process, replace part soda ash to carry out salt refining deliming using cheap saltcake, glauber salt, effectively reduce
Soda ash consumption, reduce salt refining expense.But salt refining, a large amount of Ca are carried out using the technology2+With SO4 2-Combine to form
Dihydrate gypsum simultaneously enters in a salt slurry, and by-product salt slurry is significantly increased.
The content of the invention
Present invention seek to address that the problem of background technology is present, and calcium in a kind of salt solution, magnesium are provided and removes and prepares step by step
The process units and production method of dihydrate gypsum product.
The present invention solves the technical scheme that described problem uses：
A kind of process units using saltcake refined brine and by-product dihydrate gypsum, including demagging reactor, baffling groove, demagging are clear
Clear bucket, calcium-removing reactor, deliming settling tank, demagging reactor are connected by pipeline with baffling groove I, and baffling groove I is clarified with demagging
Bucket connection, demagging reactor and demagging clarification bottom of the barrel are connected by pipeline with a salt slurry buffer barrel respectively, demagging settling tank
Overfall be connected by pipeline with demagging crude brine buffer barrel；Demagging crude brine buffer barrel passes through pipeline and demagging crude brine
Pump is connected with calcium-removing reactor, and calcium-removing reactor is connected with baffling groove II and dihydrate gypsum slurry buffer barrel respectively by pipeline,
Baffling groove II is connected with deliming settling tank, deliming settling tank by pipeline respectively with primary brine buffer barrel and dihydrate gypsum slurry
Buffer barrel is connected, and dihydrate gypsum slurry buffer barrel is connected by pipeline and dihydrate gypsum shurry pump with filter, and band filter leads to
Pipeline is crossed to be connected with primary brine buffer barrel.
Technical scheme is used by production method：
Carry out as follows：
A, crude brine is added into demagging reactor, according to the amount of magnesium ion in the crude brine for entering demagging reactor, by Mg2+：
OH-Mol ratio 1：2.06~2.16 add milk of lime into demagging reactor, utilize Ca in milk of lime (OH)2With Mg in crude brine2 +Reaction forms Mg (OH)2；Reaction solution enters demagging settling tank through baffling groove I and carries out clarifying treatment, from demagging clarification bottom of the barrel and
Salt mud of demagging reactor bottom outflow enters a salt slurry buffer barrel, crude salt mud treatment process is sent to, after processing
Carry out recycling；High calcium clear liquid after demagging is as demagging crude brine from the top overflow of demagging settling tank to demagging crude brine
Buffer barrel, realize crude brine demagging；
B, the demagging crude brine from demagging crude brine buffer barrel is pumped into calcium-removing reactor through demagging crude brine, thick according to demagging
The total amount of calcium ion in salt solution, by 1：0.95~1.1 mol ratio adds metabisulfite solution into calcium-removing reactor；Reacted in deliming
In device, the Ca in demagging crude brine 2+There are 58~71% and SO4 2-Combine to form dihydrate gypsum crystallization；Reaction solution enters through baffling groove II
Enter deliming settling tank and carry out clarifying treatment, the underflow material of the crystallization containing dihydrate gypsum clarifies bottom of the barrel stream from calcium-removing reactor and deliming
Go out, into dihydrate gypsum slurry buffer barrel, the low calcium clear liquid that the top overflow of deliming settling tank goes out flow to one certainly as primary brine
Secondary buffered saline bucket, realize crude brine mirabilite method deliming；
C, the dihydrate gypsum underflow material in dihydrate gypsum slurry buffer barrel, with dihydrate gypsum material pulp pumping to band filter, through solid-liquid
Separation, washing drop chlorine, output dihydrate gypsum product, band filter filtrate enter primary brine buffer barrel together with deliming crude brine,
It is pumped into by primary brine and carries out depth deliming into next process；Drop chlorine washings are re-circulated into soda manufacture system
System.
The present invention is compared with prior art：Lime demagging, the step-by-step processing technology of saltcake deliming, and by dihydrate gypsum solid-liquid
Isolation technics incorporates wherein, using saltcake refined brine while the integral manufacturing technique of by-product dihydrate gypsum, realizes salt crystal
The further minimizing of byproduct in process salt slurry processed, and the dihydrate gypsum product for having added value is obtained from abandoned salty mud, realize
Turn waste into wealth.The dihydrate gypsum crystalline particle of formation uniformly, beneficial to modification, whiteness reaches more than 92%, and purity is long more than 96%
Footpath is than 5~10, product grade height, steady quality, excellent performance, crystal formation can be prepared by technology controlling and process, granularity meets production α
Type high strength gypsum, β type gypsum are beautiful applied to ceramics, hot investment casting, medical, aviation, ship, automobile, plastics, building and technique
The fields such as art；The invention provides a kind of recycling new way of ammonia-soda process soda manufacture waste discharge salt slurry, is ammonia alkali enterprise
Sustainable development provide technical support.
The preferred scheme of production method：
Mg (OH) in a salt slurry composition in step a2Account for mass ratio 16~16.5%, CaSO4.2H2O accounts for 14.5~15%, crude salt
The water-insoluble in biological sludge in industrial and milk of lime in water accounts for 16.5~17.5%, moisture content 48~52%；Salt slurry sedimentation
To demagging reactor and demagging clarification bottom of the barrel, and a salt slurry buffer barrel is drained into a salt slurry form, one time salt slurry accounts for
The 1/50~1/60 of reaction solution gross mass in demagging reactor.
Material reacts generation crystallization in calcium-removing reactor and controlled at 100 points the total time of crystal growth in step b
Clock or so, at 40~45 DEG C, speed of agitator is controlled in 18r/min for reaction temperature control.
In step b, the CaSO that is generated in calcium-removing reactor4.2H2O is accounted for into the total matter of material reaction liquid in calcium-removing reactor
The 0.4%~0.6% of amount.
In step b, the underflow material of the dihydrate gypsum crystallization in deliming settling tank is accounted for into demagging reactor and deliming reaction
3.5%~5% of material reaction liquid gross mass within both devices.
Brief description of the drawings
Fig. 1 is the structural representation of the present invention.
Embodiment
Below in conjunction with the accompanying drawings and embodiment states the present invention：
Embodiment one：
A kind of process units using saltcake refined brine and by-product dihydrate gypsum, referring to accompanying drawing, in figure：1- demagging reactors,
2- bafflings groove I, 3- demagging settling tanks, 4- calcium-removing reactors, 5- bafflings groove II, 6- deliming settling tanks, 7- primary brine buffer barrels,
8- primary brine pumps, 9- band filters, 10- dihydrate gypsum shurry pumps, 11- dihydrate gypsum slurry buffer barrels, 12- demagging crude brines
Pump, 13- demagging crude brine buffer barrels, salt slurry buffer barrel of 14-, salt dredge pump of 15-.
Demagging reactor 1 is connected by pipeline with baffling groove I 2, and baffling groove I 2 is connected with demagging settling tank 3, except reactive magnesium
Device 1 and the bottom of demagging settling tank 3 are connected by pipeline with a salt slurry buffer barrel 14 respectively, and one time salt slurry buffer barrel 14 passes through pipe
Road is connected with a salt dredge pump 15.
The overfall of demagging settling tank 3 is connected by pipeline with demagging crude brine buffer barrel 13；Demagging crude brine buffer barrel
13 are connected by pipeline and demagging crude salt water pump 12 with calcium-removing reactor 4, calcium-removing reactor 4 by pipeline respectively with baffling groove
II 5 and dihydrate gypsum slurry buffer barrel 11 connect, baffling groove II 5 is connected with deliming settling tank 6, and deliming settling tank 6 passes through pipeline
It is connected respectively with primary brine buffer barrel 14 and dihydrate gypsum slurry buffer barrel 11, dihydrate gypsum slurry buffer barrel 11 passes through pipeline
And dihydrate gypsum shurry pump 10 is connected with filter 9, band filter 9 is connected by pipeline with primary brine buffer barrel 7.
In the present embodiment, by Mg in crude brine2+：OH in milk of lime-1：2.06 mol ratio adds into demagging reactor 1
Enter crude brine, milk of lime, carry out removing reactive magnesium under agitation, the Mg in crude brine2+All with the OH in milk of lime-With reference to
Into Mg (OH)2, meanwhile, the Ca in reaction solution2+Have 5~15%（Mol ratio）With SO4 2-It is combined into CaSO4.2H2O.Except reactive magnesium
The Mg (OH) formed in device 12、CaSO4.2H2O, the material such as water-insoluble in the biological sludge in industrial and milk of lime in crude brine.
Mg (OH) in salt slurry composition2Account for mass ratio 16.5%, CaSO4.2H2O accounts for 15%, biological sludge in industrial and lime in crude brine
Water-insoluble in breast accounts for 17.5%, moisture content 51%.
Salt Fender sub-fraction is settled down to the bottom of demagging reactor 1 with solution after reaction in the lump with a salt mud shape
Formula（Wherein, a salt slurry accounts for the 1/50 of reaction solution gross mass）Drain into outside a salt slurry buffer barrel 14, remaining major part is with anti-
Solution enters the progress clarifying treatment of demagging settling tank 3 through baffling groove I 2 after answering, and in demagging settling tank 3, is pressed from both sides after reaction in solution
The Mg (OH) of band2、CaSO4.2H2O, the water-insoluble in the biological sludge in industrial and milk of lime in crude brine is settled down to bottom, with one
The form of secondary salt mud（One time salt mud accounts for 8% of reaction solution gross mass in demagging reactor 1,）Drain into a salt slurry buffering
Bucket 14, pumped through a salt slurry toward salt slurry press filtration process, clear liquid is as demagging crude brine from the top overflow of demagging settling tank 3 to removing
In magnesium crude brine buffer barrel 13.
Demagging crude brine in demagging crude brine buffer barrel 13 is sent into calcium-removing reactor 4 through demagging crude salt water pump 12, simultaneously
Metabisulfite solution is added into calcium-removing reactor 4（The SO into the metabisulfite solution of calcium-removing reactor 44 2-Mole is removed with entering
Ca in the demagging crude brine of calcium reactor 42+Mole ratio is 1：1.1）.Ca in demagging crude brine2+Have 58~71%（Mole
Than）With SO4 2-Combine to form dihydrate gypsum crystallization.
In calcium-removing reactor 4, the total time of material reaction generation crystallization and crystal growth is controlled at 100 minutes or so,
At 40~45 DEG C, speed of agitator is controlled in 18r/min for reaction temperature control.
In calcium-removing reactor 4, a small amount of CaSO4.2H2O（Account for 1/200 of reaction solution gross mass in calcium-removing reactor 4）It is heavy
It is down to bottom and dihydrate gypsum slurry buffer barrel 11 is drained into the form of dihydrate gypsum slurry；Remaining most of reaction solution is through baffling groove II
5 enter the cylindrical central sleeve of deliming settling tank 6, and solid-liquid sedimentation separation is carried out in deliming settling tank 6, are crystallized containing dihydrate gypsum dense
Slurry（Account for 4% or so of both demagging reactor 1 and calcium-removing reactor 4 reaction solution gross masses）Flowed from the bottom of deliming settling tank 6
Go out, into dihydrate gypsum slurry buffer barrel 11, the low calcium clear liquid that the top overflow of deliming settling tank 6 goes out is flow to certainly as primary brine
Primary brine buffer barrel 7, then the primary brine soda ash deliming process in soda manufacture device area is delivered to through primary brine pump 8, carry out
Depth deliming, realize demagging crude brine mirabilite method deliming.
Dihydrate gypsum slurry in dihydrate gypsum slurry buffer barrel 11 is delivered in band filter 9 through dihydrate gypsum shurry pump 10
Row separation of solid and liquid, washing drop chlorine, complete dihydrate gypsum preparation process.The filtrate and deliming that dihydrate gypsum slurry separation of solid and liquid is formed
The clear liquid of the top overflow of settling tank 6 enters primary brine buffer barrel 7 together.The two water stones that dihydrate gypsum slurry separation of solid and liquid is formed
Cream filter cake can be handled through turning the deep process such as brilliant, modified, dehydration, produce the high alpha type high-strength gypsum of added value, β type stones
Cream.Washings caused by dihydrate gypsum Washing of Filter Cake drop chlorine process are re-circulated into soda manufacture system.
Embodiment two：
By Mg in crude brine2+：OH in milk of lime-1：2.16 mol ratio adds crude brine, milk of lime into demagging reactor 1,
Carry out removing reactive magnesium under agitation, the Mg in crude brine2+All with the OH in milk of lime-It is combined into Mg (OH)2, meanwhile,
There is the Ca of 10% mol ratio in reaction solution2+With SO4 2-It is combined into CaSO4.2H2O.The Mg (OH) formed in demagging reactor 12、
CaSO4.2H2O, the material such as water-insoluble in the biological sludge in industrial and milk of lime in crude brine.Mg in salt slurry composition
(OH)2Account for mass ratio 16%, CaSO4.2H2O accounts for 14.5%, water-insoluble in biological sludge in industrial and milk of lime in crude brine etc.
16.5% is accounted for for other impurity, moisture content 52%.
Salt Fender sub-fraction is settled down to the bottom of demagging reactor 1 with solution after reaction in the lump with a salt mud shape
Formula（Wherein, a salt slurry accounts for the 1/50 of reaction solution gross mass）Drain into outside a salt slurry buffer barrel 14, remaining major part is with anti-
Solution enters the progress clarifying treatment of demagging settling tank 3 through baffling groove I 2 after answering, and in demagging settling tank 3, is pressed from both sides after reaction in solution
The Mg (OH) of band2、CaSO4.2H2O, the water-insoluble in the biological sludge in industrial and milk of lime in crude brine is settled down to bottom, with one
The form of secondary salt mud（One time salt mud accounts for 8.1% of reaction solution gross mass in demagging reactor 1,）A salt slurry is drained into delay
Rush bucket 14, pumped through a salt slurry toward salt slurry press filtration process, clear liquid as demagging crude brine from the top overflow of demagging settling tank 3 extremely
In demagging crude brine buffer barrel 13.
Demagging crude brine in demagging crude brine buffer barrel 13 is sent into calcium-removing reactor 4 through demagging crude salt water pump 12, simultaneously
Metabisulfite solution is added into calcium-removing reactor 4（The SO into the metabisulfite solution of calcium-removing reactor 44 2-Mole is removed with entering
Ca in the demagging crude brine of calcium reactor 42+Mole ratio is 1：1.1）.Ca in demagging crude brine2+Have 65%（Mol ratio）
With SO4 2-Combine to form dihydrate gypsum crystallization.
In calcium-removing reactor 4, the total time of material reaction generation crystallization and crystal growth is controlled at 100 minutes or so,
At 40~45 DEG C, speed of agitator is controlled in 18r/min for reaction temperature control.
In calcium-removing reactor 4, a small amount of CaSO4.2H2O（Account for 1/220 of reaction solution gross mass in calcium-removing reactor 4）It is heavy
It is down to bottom and dihydrate gypsum slurry buffer barrel 11 is drained into the form of dihydrate gypsum slurry；Remaining most of reaction solution is through baffling groove II
5 enter the cylindrical central sleeve of deliming settling tank 6, and solid-liquid sedimentation separation is carried out in deliming settling tank 6, are crystallized containing dihydrate gypsum dense
Slurry（Account for 4% or so of both demagging reactor 1 and calcium-removing reactor 4 reaction solution gross masses）Flowed from the bottom of deliming settling tank 6
Go out, into dihydrate gypsum slurry buffer barrel 11, the low calcium clear liquid that the top overflow of deliming settling tank 6 goes out is flow to certainly as primary brine
Primary brine buffer barrel 7, then the primary brine soda ash deliming process in soda manufacture device area is delivered to through primary brine pump 8, carry out
Depth deliming, realize demagging crude brine mirabilite method deliming.
Dihydrate gypsum slurry in dihydrate gypsum slurry buffer barrel 11 is delivered in band filter 9 through dihydrate gypsum shurry pump 10
Row separation of solid and liquid, washing drop chlorine, complete dihydrate gypsum preparation process.The filtrate and deliming that dihydrate gypsum slurry separation of solid and liquid is formed
The clear liquid of the top overflow of settling tank 6 enters primary brine buffer barrel 7 together.The two water stones that dihydrate gypsum slurry separation of solid and liquid is formed
Cream filter cake can be handled through turning the deep process such as brilliant, modified, dehydration, produce the high alpha type high-strength gypsum of added value, β type stones
Cream.Washings caused by dihydrate gypsum Washing of Filter Cake drop chlorine process are re-circulated into soda manufacture system.
Compared with brine rectification process patented technology, using the technology of the present invention, the dihydrate gypsum in a salt slurry is carried out
Recycle, cut down the yield for discarding salt slurry 35% or so, and greatly improve magnesium hydroxide in abandoned salty mud
Content, develop a set of magnesium products for next step salt slurry and create more preferably condition.
Using an output salt solution before and after the technology of the present invention and waste discharge salt slurry data comparison：
Claims (6)
1. a kind of process units using saltcake refined brine and by-product dihydrate gypsum, including demagging reactor, baffling groove I, remove
Magnesium settling tank, a salt slurry buffer barrel, demagging crude brine buffer barrel, calcium-removing reactor, baffling groove II, deliming settling tank, two water
Gypsum slurry buffer barrel, band filter, primary brine buffer barrel, a salt dredge pump, demagging crude salt water pump, dihydrate gypsum shurry pump,
Primary brine pump；It is characterized in that：Demagging reactor is connected by pipeline with baffling groove I, and baffling groove I connects with demagging settling tank
Connect, demagging reactor and demagging clarification bottom of the barrel are connected by pipeline with a salt slurry buffer barrel respectively, and demagging settling tank overflows
Head piece is connected by pipeline with demagging crude brine buffer barrel；Demagging crude brine buffer barrel by pipeline and demagging crude salt water pump with
Calcium-removing reactor is connected, and calcium-removing reactor is connected with baffling groove II and dihydrate gypsum slurry buffer barrel respectively by pipeline, baffling
Groove II is connected with deliming settling tank, and deliming settling tank is buffered with primary brine buffer barrel and dihydrate gypsum slurry respectively by pipeline
Bucket connection, dihydrate gypsum slurry buffer barrel are connected by pipeline and dihydrate gypsum shurry pump with filter, and band filter passes through pipe
Road is connected with primary brine buffer barrel.
2. a kind of method of production saltcake refined brine of process units as claimed in claim 1 and by-product dihydrate gypsum, by as follows
Step is carried out：
A, crude brine is added into demagging reactor, according to the amount of magnesium ion in the crude brine for entering demagging reactor, by Mg2+：
OH-Mol ratio 1：2.06~2.16 add milk of lime into demagging reactor, utilize Ca in milk of lime (OH)2With Mg in crude brine2 +Reaction forms Mg (OH)2；Reaction solution enters demagging settling tank through baffling groove I and carries out clarifying treatment, from demagging clarification bottom of the barrel and
Salt mud of demagging reactor bottom outflow enters a salt slurry buffer barrel, crude salt mud treatment process is sent to, after processing
Carry out recycling；High calcium clear liquid after demagging is as demagging crude brine from the top overflow of demagging settling tank to demagging crude brine
Buffer barrel, realize crude brine demagging；
B, the demagging crude brine from demagging crude brine buffer barrel is pumped into calcium-removing reactor through demagging crude brine, thick according to demagging
The total amount of calcium ion in salt solution, by 1：0.95~1.1 mol ratio adds metabisulfite solution into calcium-removing reactor；Reacted in deliming
In device, the Ca in demagging crude brine 2+There are 58~71% and SO4 2-Combine to form dihydrate gypsum crystallization；Reaction solution enters through baffling groove II
Enter deliming settling tank and carry out clarifying treatment, the underflow material of the crystallization containing dihydrate gypsum clarifies bottom of the barrel stream from calcium-removing reactor and deliming
Go out, into dihydrate gypsum slurry buffer barrel, the low calcium clear liquid that the top overflow of deliming settling tank goes out flow to one certainly as primary brine
Secondary buffered saline bucket, realize crude brine mirabilite method deliming；
C, the dihydrate gypsum underflow material in dihydrate gypsum slurry buffer barrel, with dihydrate gypsum material pulp pumping to band filter, through solid-liquid
Separation, washing drop chlorine, output dihydrate gypsum product, band filter filtrate enter primary brine buffer barrel together with deliming crude brine,
It is pumped into by primary brine and carries out depth deliming into next process；Drop chlorine washings are re-circulated into soda manufacture system
System.
3. the method for process units production saltcake refined brine according to claim 2 and by-product dihydrate gypsum, its feature
It is：Mg (OH) in a salt slurry composition in step a2Account for mass ratio 16~16.5%, CaSO4.2H2O accounts for 14.5~15%, crude salt
The water-insoluble in biological sludge in industrial and milk of lime in water accounts for 16.5~17.5%, moisture content 48~52%；Salt slurry sedimentation
To demagging reactor and demagging clarification bottom of the barrel, and a salt slurry buffer barrel is drained into a salt slurry form, one time salt slurry accounts for
The 1/50~1/60 of reaction solution gross mass in demagging reactor.
4. the method for process units production saltcake refined brine according to claim 2 and by-product dihydrate gypsum, its feature
It is：Material reacts generation crystallization in calcium-removing reactor and controlled on 100 minutes left sides the total time of crystal growth in step b
The right side, at 40~45 DEG C, speed of agitator is controlled in 18r/min for reaction temperature control.
5. the method for process units production saltcake refined brine according to claim 2 and by-product dihydrate gypsum, its feature
It is：In step b, the CaSO that is generated in calcium-removing reactor4.2H2O is accounted for into the material reaction liquid gross mass in calcium-removing reactor
0.4%~0.6%.
6. the method for process units production saltcake refined brine according to claim 2 and by-product dihydrate gypsum, its feature
It is：In step b, the underflow material of the dihydrate gypsum crystallization in deliming settling tank is accounted for into demagging reactor and calcium-removing reactor two
3.5%~5% of material reaction liquid gross mass within person.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711493077.7A CN107892313A (en) | 2017-12-30 | 2017-12-30 | Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711493077.7A CN107892313A (en) | 2017-12-30 | 2017-12-30 | Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107892313A true CN107892313A (en) | 2018-04-10 |
Family
ID=61808935
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711493077.7A Pending CN107892313A (en) | 2017-12-30 | 2017-12-30 | Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107892313A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109485083A (en) * | 2018-12-20 | 2019-03-19 | 四川久大蓬莱盐化有限公司 | A kind of preparation method and preparation system of feed addictive calcium sulfate |
| CN111777081A (en) * | 2020-07-16 | 2020-10-16 | 江苏新源矿业有限责任公司 | Wastewater zero-discharge treatment process and device suitable for calcium sulfate whisker production |
| CN112429896A (en) * | 2020-10-29 | 2021-03-02 | 河南佰利联新材料有限公司 | Treatment method of salt mud produced in chlor-alkali production |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU735566A1 (en) * | 1972-03-23 | 1980-05-25 | Предприятие П/Я А-7125 | Method of purifying natural liquor from magnesium and calcium |
| CN102795719A (en) * | 2011-05-27 | 2012-11-28 | 王凯勋 | Methods for removing calcium and magnesium and co-producing water and salt by low-cost process during sea water desalination |
| CN102951659A (en) * | 2012-12-06 | 2013-03-06 | 唐山三友化工股份有限公司 | Method for preparing refined brine and methods for preparing byproducts thereofof refined brine |
| CN103950957A (en) * | 2014-04-22 | 2014-07-30 | 彭振超 | Process method for preparing magnesium hydroxide from magnesium sulfate |
| CN104959012A (en) * | 2015-04-17 | 2015-10-07 | 熊天渝 | Magnesium-calcium based wet method desulphurization system and method for removing sulfur dioxide in flue gas and producing gypsum |
| CN107089675A (en) * | 2017-05-27 | 2017-08-25 | 石家庄科林威尔环保科技有限公司 | A kind of new method for the distilled ammonia wastewater recycling that ammonia-soda process soda ash is discharged |
| CN207671700U (en) * | 2017-12-30 | 2018-07-31 | 唐山三友化工股份有限公司 | Utilize saltcake refined brine and the process units of by-product dihydrate gypsum |
-
2017
- 2017-12-30 CN CN201711493077.7A patent/CN107892313A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU735566A1 (en) * | 1972-03-23 | 1980-05-25 | Предприятие П/Я А-7125 | Method of purifying natural liquor from magnesium and calcium |
| CN102795719A (en) * | 2011-05-27 | 2012-11-28 | 王凯勋 | Methods for removing calcium and magnesium and co-producing water and salt by low-cost process during sea water desalination |
| CN102951659A (en) * | 2012-12-06 | 2013-03-06 | 唐山三友化工股份有限公司 | Method for preparing refined brine and methods for preparing byproducts thereofof refined brine |
| CN103950957A (en) * | 2014-04-22 | 2014-07-30 | 彭振超 | Process method for preparing magnesium hydroxide from magnesium sulfate |
| CN104959012A (en) * | 2015-04-17 | 2015-10-07 | 熊天渝 | Magnesium-calcium based wet method desulphurization system and method for removing sulfur dioxide in flue gas and producing gypsum |
| CN107089675A (en) * | 2017-05-27 | 2017-08-25 | 石家庄科林威尔环保科技有限公司 | A kind of new method for the distilled ammonia wastewater recycling that ammonia-soda process soda ash is discharged |
| CN207671700U (en) * | 2017-12-30 | 2018-07-31 | 唐山三友化工股份有限公司 | Utilize saltcake refined brine and the process units of by-product dihydrate gypsum |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109485083A (en) * | 2018-12-20 | 2019-03-19 | 四川久大蓬莱盐化有限公司 | A kind of preparation method and preparation system of feed addictive calcium sulfate |
| CN111777081A (en) * | 2020-07-16 | 2020-10-16 | 江苏新源矿业有限责任公司 | Wastewater zero-discharge treatment process and device suitable for calcium sulfate whisker production |
| CN112429896A (en) * | 2020-10-29 | 2021-03-02 | 河南佰利联新材料有限公司 | Treatment method of salt mud produced in chlor-alkali production |
| CN112429896B (en) * | 2020-10-29 | 2022-10-25 | 河南佰利联新材料有限公司 | Treatment method of salt mud produced in chlor-alkali production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108128961A (en) | Brine waste zero emission method and system | |
| CN105439105A (en) | Integrated membrane treatment and recovery technology and apparatus for waste acid in production process of titanium dioxide | |
| CN101628722B (en) | Process for refining crude salt | |
| CN107892313A (en) | Utilize saltcake refined brine and the process units and production method of by-product dihydrate gypsum | |
| CN105002306B (en) | A kind of syrup is without sulfur highly effective purification method | |
| CN102795719A (en) | Methods for removing calcium and magnesium and co-producing water and salt by low-cost process during sea water desalination | |
| CN105858692A (en) | Method for treating magnesium sulfate and magnesium sulfite wastewater by virtue of lime method | |
| CN103058853B (en) | A kind of production method of calcium hydrogen citrate | |
| CN101293849A (en) | Process for preparing glutamic acid crystallization | |
| CN102951668B (en) | Method for co-producing calcium sulphate and magnesium hydrate by ammonia alkali waste liquid and concentrated seawater | |
| CN103044239B (en) | Production method of sodium citrate | |
| CN114988380A (en) | Method for producing food-grade monopotassium phosphate and co-producing high-purity gypsum by using feed-grade calcium hydrophosphate | |
| CN103880042B (en) | The method of saltcake refined brine and preventing scaring | |
| CN102351245A (en) | Continuous production method for ammonium vanadate | |
| CN207671700U (en) | Utilize saltcake refined brine and the process units of by-product dihydrate gypsum | |
| CN112850758A (en) | Lithium extraction system and method for salt lake brine | |
| CN101844781B (en) | Manufacturing technique of high-purity thenardite | |
| CN112919506B (en) | Device and method for continuously producing lithium chloride from salt lake lithium-rich brine | |
| CN112919505B (en) | Device and method for continuously producing lithium hydroxide from salt lake lithium-rich brine | |
| CN209493410U (en) | Remove the device of whole hardness in reverse osmosis concentrated water | |
| CN205973831U (en) | Environment -friendly ammonia -soda process soda ash production system | |
| CN106629792A (en) | Co-production technology for preparing high-purity magnesium hydrate and preparing calcium sulfate whiskers from magnesium hydrate production byproduct | |
| CN114804435A (en) | Wastewater treatment method for desalting by using glauberite technology | |
| CN106673026A (en) | Process for preparing crystal whisker calcium carbonate through combined production of high-purity magnesium hydrate and by-product | |
| CN209797627U (en) | Processing apparatus of strong brine that contains high concentration calcium sulfate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |