CN112897551A - Novel vacuum salt making and discharging process - Google Patents
Novel vacuum salt making and discharging process Download PDFInfo
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- CN112897551A CN112897551A CN202011473452.3A CN202011473452A CN112897551A CN 112897551 A CN112897551 A CN 112897551A CN 202011473452 A CN202011473452 A CN 202011473452A CN 112897551 A CN112897551 A CN 112897551A
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- 150000003839 salts Chemical class 0.000 title claims abstract description 210
- 238000000034 method Methods 0.000 title claims abstract description 31
- 230000008569 process Effects 0.000 title claims abstract description 27
- 238000007599 discharging Methods 0.000 title claims abstract description 13
- 239000002002 slurry Substances 0.000 claims abstract description 50
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 44
- 239000002562 thickening agent Substances 0.000 claims abstract description 40
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 38
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 38
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910001868 water Inorganic materials 0.000 claims abstract description 26
- 239000011780 sodium chloride Substances 0.000 claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- 239000012452 mother liquor Substances 0.000 claims abstract description 19
- 238000004364 calculation method Methods 0.000 claims description 15
- 230000008018 melting Effects 0.000 claims description 13
- 238000002844 melting Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 10
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 9
- 239000012267 brine Substances 0.000 claims description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 6
- 238000003306 harvesting Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000010409 thin film Substances 0.000 claims description 4
- 238000006386 neutralization reaction Methods 0.000 claims description 3
- 230000008878 coupling Effects 0.000 claims description 2
- 238000010168 coupling process Methods 0.000 claims description 2
- 238000005859 coupling reaction Methods 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 abstract description 3
- 230000008020 evaporation Effects 0.000 abstract description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 238000005457 optimization Methods 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 230000002159 abnormal effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 150000007523 nucleic acids Chemical class 0.000 description 1
- 102000039446 nucleic acids Human genes 0.000 description 1
- 108020004707 nucleic acids Proteins 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000017260 vegetative to reproductive phase transition of meristem Effects 0.000 description 1
Images
Classifications
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- 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
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Metallurgy (AREA)
- Seasonings (AREA)
Abstract
The invention provides a novel vacuum salt making and discharging process, which comprises a salt thickener and a salt dissolving pool, wherein the salt thickener is connected with the salt dissolving pool through a pipeline, the pipeline between the salt thickener and the salt dissolving pool is respectively provided with a valve and a flowmeter, the salt slurry at the bottom of the salt thickener consists of pure salt slurry and mother liquor, the mother liquor comprises sodium chloride, sodium sulfate and water, the mass concentration of the sodium sulfate in the salt dissolving pool is required to be less than 7.4g/l, the salt slurry discharged by a salt leg of an evaporation tank of a salt system is fed into a T-401 salt slurry barrel during working, the salt slurry is fed into a TH-401 salt thickener through a P-401 salt slurry pump, when the density of the salt thickener reaches 1.85T/m, the salt slurry in the salt dissolving pool is put into salt dissolving, the scheme cancels a centrifugal process and a belt conveying process at the tail end of the salt making production process, solves the problem of industrial salt loss in the production process, avoids the influence on the production caused by the fault of a belt conveyor, meanwhile, direct and indirect operation costs of the centrifuge and the belt conveyor such as power consumption, spare part consumption and the like are saved.
Description
Technical Field
The invention belongs to the technical field of salt production, and particularly relates to a novel vacuum salt production and discharge process.
Background
Salt production is the production of salt (or industrial salt), the salt production industry plays an important economic position in national economy, is an important component of national economy, salt is a necessity of human life, is a basic raw material of chemical industry, and has wide application in other industrial departments and agriculture, animal husbandry and fishery.
In the prior art, salt slurry discharged in vacuum salt production is thickened by a salt thickener, dewatered by a salt centrifuge and then conveyed to a salt dissolving pool by a salt belt, but when the comprehensive loss checking work is carried out in the salt production process, the loss of salt production capacity is found to be mainly concentrated in a centrifugal process and a belt process at the tail end of the production process:
1. salt slurry discharged from salt legs of an evaporation tank of the salt system enters a T-401 salt slurry barrel, the salt slurry is sent into a TH-401 salt thickener through a P-401 salt slurry pump, the salt slurry is further concentrated through gravity settling in the TH-401 salt thickener and then sent into a salt centrifuge for dehydration, and saturated brine mother liquor removed by the salt centrifuge returns to the T-401 salt slurry barrel. The salt slurry is highly susceptible to caking in the salt slurry barrel, and these lumps of salt may cause an overflow of salt slurry into the salt slurry barrel, with the amount of overflow salt slurry estimated to be about 15 tons per day, converted to industrial salt.
2. After being dewatered by a salt centrifuge, salt slurry falls to a No. 1 salt conveying belt through a discharge chute with the outlet of the centrifuge being as high as 6 meters, and is respectively conveyed to a salt melting pool and a scattered salt shed of a caustic soda workshop through the transportation of the No. 2 salt conveying belt and the No. 3 salt conveying belt. The industrial salt after the dehydration of the salt centrifuge contains 2.5 percent of water and is easy to adhere to the inner wall of the feeding chute, meanwhile, the feeding chute is easy to block because the feeding chute is as high as 6 meters, and the discharge of the material is not smooth because the chute is blocked, so that the salt is sprayed at the feeding opening of the centrifuge. The blocked chute was flushed every 30 minutes by the centrifugation station staff. The salt scraping effect of the salt conveying belt is poor due to the fact that the salt scraping belt is charged with water, and then salt falling of the belt is serious. The salt is sprayed at the feed opening and the water carried by the belt conveyor is scattered to cause the loss of about 10 tons of industrial salt every day.
3. When the salt conveying belt has abnormal faults and needs to be overhauled, the whole system of the salt manufacturing workshop is stopped because no standby belt exists. Due to the particularity of the vacuum salt production process, the concentration, saturation and crystallization of the feed liquid need a certain time, industrial salt products can be produced only after about 10 hours after normal start, and the full-load state can be reached only after about 15 hours, so that the loss of industrial salt is about 1000 tons due to the abnormal failure of the salt conveying belt at one time.
The invention aims to solve the problem of how to reduce the loss of salt making capacity during the work of the salt making production process.
Disclosure of Invention
The invention aims to provide a novel vacuum salt making and discharging process to solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme: a novel vacuum salt making and discharging process comprises a salt thickener and a salt dissolving pool, wherein the salt thickener is connected with the salt dissolving pool through a pipeline, a valve and a flowmeter are respectively arranged on the pipeline between the salt thickener and the salt dissolving pool, salt slurry at the bottom of the salt thickener consists of pure salt slurry and mother liquor, the mother liquor comprises sodium chloride, sodium sulfate and water, the mass concentration of the sodium sulfate in the salt dissolving pool is less than 7.4g/l, and the mass concentration of the sodium sulfate in the salt dissolving pool is required to be less than 7.4 g/l.
As optimization, pure salt slurry: volume ratio of mother liquor is 66%:34% under thin-film high pressure, high pressure.
Preferably, the mass concentration of sodium chloride is b, the mass concentration of sodium sulfate is c, b =290g/l-300g/l, c =18 g/l-24g/l, the mass concentration of sodium chloride in the salt pond is d, and d =290g/l-310 g/l.
As optimization, the calculation formula of the mass concentration of sodium sulfate in the salt pond is as follows:
1 t/m³=1000 g/L；
in the salt thickener, the calculation formula of sodium chloride in each cubic salt slurry is as follows:
E=66%*a+34%*b；
in the salt thickener, the calculation formula of sodium sulfate in each cubic salt slurry is as follows:
F=34%*c；
the water demand calculation formula under d mass concentration after the salt dissolving pool is neutralized into salt water is as follows:
G=E/d-0.34；
the theoretical sodium sulfate content calculation formula after the salt dissolving pool is neutralized into salt water is as follows:
H= F/G。
as an optimization, under the conditions of a =1.85t/m, b =290g/l, c =20g/l, and d =300g/l, the theoretical sodium sulfate content after neutralization to brine in the salt pond is:
each cubic salt slurry contains sodium chloride: e = 66%. 1.85+ 34%. 0.29=1.32 t;
sodium sulfate per cubic salt slurry: f =34% + 0.02=0.0068 t;
water requirement for 300g/l of saline water: (iii) thin film obtained by ethanol harvest at G =1.32/0.3-0.34=4.06 m;
theoretical sodium sulfate content after conversion to brine:
h =0.0068/4.06=0.00167 tonnes/m cultivation =1.67 g/l.
For optimization, H is less than 7.4 g/l.
According to the invention, the sodium sulfate content of the salt slurry saturated mother liquor is continuously sampled and analyzed, and the salt slurry analysis result is as follows:
the salt slurry at the bottom of the thickener consists of about 66 percent of pure salt slurry and about 34 percent of mother liquor, wherein the measured density of the salt slurry is 1.85t/m, the mother liquor contains 300g/l of sodium chloride with the value of 290-24 g/l, the rest part of the mother liquor is water, and the sodium chloride concentration after salt dissolution is 310g/l with the value of 290-, thereby calculating the following steps:
each cubic salt slurry contains sodium chloride: 0.66 x 1.85+0.34 x 0.29=1.32 t;
sodium sulfate per cubic salt slurry: 0.34 × 0.02=0.0068 t;
water requirement for 300g/l of saline water: performing a heavy harvest at 1.32/0.3-0.34=4.06 m;
theoretical sodium sulfate content after conversion to brine:
0.0068/4.06=0.00167 ton/m thin flowering under stress =1.67 g/l.
After the conversion into brine, the theoretical sodium sulfate content is far lower than the requirement that the sodium sulfate content in a salt melting pool is less than 7.4g/l, and the method is completely feasible theoretically.
Compared with the prior art, the invention has the beneficial effects that:
(1) after determining that the sulfate radical content of the saturated mother liquor of the salt slurry can meet the production requirements of a caustic soda workshop, the salt manufacturing workshop provides a bold scheme-a centrifugal process and a belt conveying process are cancelled on the basis, the salt slurry is directly discharged into a salt melting pool of the caustic soda workshop from a salt thickener, the centrifugal process and the belt conveying process at the tail end of the salt manufacturing production process are cancelled, the problem of industrial salt loss in the production process is solved, adverse effects on production caused by belt conveyor faults are avoided, and direct and indirect operation costs of a centrifuge and a belt conveyor such as power consumption, spare part consumption and the like are saved;
(2) analyzing the components of the salt slurry, under the condition of ensuring that the content of sodium sulfate does not exceed the index, canceling a vacuum salt-making centrifugal process and a belt conveying process, and directly discharging the salt slurry into a salt dissolving pool of a caustic soda workshop from the lower part of a salt thickener;
(3) and (3) reducing power consumption: centrifugal machines and belts are cancelled, a large amount of electric energy is saved, taking Hua-plastic shares as an example, the total power of three centrifugal machines is 405KW, the power of two belts is 13KWh, and only the electricity is saved by more than 200 ten thousand KWh each year;
reduction of salt loss: the invention reduces the transportation link and the loss due to the reduction of equipment maintenance, takes Hua-Mo company as an example, the loss of industrial salt is reduced by 25 tons every day, and the loss of industrial salt is estimated to be reduced by about 8000 tons all the year round.
Drawings
FIG. 1 is a schematic view of the overall structure of a novel vacuum salt production and discharge process of the present invention;
FIG. 2 is a schematic structural diagram of a new vacuum salt-making and salt-discharging process in the prior art.
In the figure: 1-salt thickener, 2-salt dissolving pool, 3-valve and 4-flowmeter.
Detailed Description
The present invention will be further illustrated with reference to the accompanying drawings and specific embodiments, which are to be understood as merely illustrative of the invention and not as limiting the scope of the invention. It should be noted that the terms "front," "back," "left," "right," "upper" and "lower" used in the following description refer to directions in the drawings, and the terms "inner" and "outer" refer to directions toward and away from, respectively, the geometric center of a particular component.
Referring to fig. 1-2, a new vacuum salt making and discharging process includes a salt thickener 1 and a salt dissolving tank 2, wherein the salt thickener 1 and the salt dissolving tank 2 are connected through a pipeline, a valve 3 and a flow meter 4 are respectively arranged on the pipeline between the salt thickener 1 and the salt dissolving tank 2, salt slurry at the bottom of the salt thickener 1 is composed of pure salt slurry and mother liquor, the mother liquor includes sodium chloride, sodium sulfate and water, the mass concentration of the sodium sulfate in the salt dissolving tank 2 is less than 7.4g/l, the valve 3 is a valve with the model of Z41H/Y/W, the flow meter 4 is a flow meter with the model of LWGY-MIK, the salt thickener 1 is a thickener with the model of "and the salt dissolving tank 2 is a flow meter with the model of LWGY-MIK.
Pure salt slurry: and (3) carrying out nucleic acid amplification on the pulp by using a pulp obtained by the method, wherein the volume ratio of the mother liquor is 66% to 34%, the density of the pulp is a, and a =1.85 t/m.
The mass concentration of sodium chloride is b, the mass concentration of sodium sulfate is c, b =290g/l-300g/l, c =18 g/l-24g/l, the mass concentration of sodium chloride in the salt pond 2 is d, and d =290g/l-310 g/l.
The calculation formula of the mass concentration of sodium sulfate in the salt dissolving tank 2 is as follows:
1 t/m³=1000 g/L；
in the salt thickener 1, the calculation formula of sodium chloride in each cubic salt slurry is as follows:
E=66%*a+34%*b；
in the salt thickener 1, the calculation formula of sodium sulfate in each cubic salt slurry is as follows:
F=34%*c；
the water demand calculation formula under the mass concentration d after the salt dissolving pool 2 is neutralized into salt water is as follows:
G=E/d-0.34；
the theoretical sodium sulfate content calculation formula after the salt dissolving pool 2 is neutralized into salt water is as follows:
H= F/G。
performing a full harvest under the conditions of a =1.85t/m, b =290g/l, c =20g/l, and d =300g/l, the theoretical sodium sulfate content after neutralization to brine in the salt pond 2 is:
each cubic salt slurry contains sodium chloride: e = 66%. 1.85+ 34%. 0.29=1.32 t;
sodium sulfate per cubic salt slurry: f =34% + 0.02=0.0068 t;
water requirement for 300g/l of saline water: (iii) thin film obtained by ethanol harvest at G =1.32/0.3-0.34=4.06 m;
theoretical sodium sulfate content after conversion to brine:
h =0.0068/4.06=0.00167 tonnes/m cultivation =1.67 g/l.
H＜7.4g/l。
The working principle is as follows: the utility model provides a new salt technology is gone out in vacuum system salt, including salt thickener 1 and salt melting pond 2, salt thickener 1 and salt melting pond 2 pass through the tube coupling, be equipped with valve 3 and flowmeter 4 on the pipeline between salt thickener 1 and the salt melting pond 2 respectively, the salt thick liquid of salt thickener 1 bottom comprises pure salt thick liquid and mother liquor, the mother liquor includes sodium chloride, sodium sulfate and water, sodium sulfate mass concentration is less than 7.4g/l in salt melting pond 2, the during operation salt system evaporating pot salt leg is arranged salt thick liquid and is gone into T-401 salt thick liquid bucket, the salt thick liquid is sent into TH-401 salt thickener through P-401 salt thick liquid pump again, when salt thickener 1 density reaches 1.85T/m year, put the salt thick liquid in the salt thickener 1 into salt melting pond 2 and carry out the salt melting.
It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents, and it is intended that the described embodiments of the invention be construed as merely a subset of the embodiments of the invention and not as a whole. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Claims (6)
1. A novel vacuum salt making and discharging process is characterized in that: including salt thickener (1) and salt melting pond (2), salt thickener (1) and salt melting pond (2) pass through the tube coupling, be equipped with valve (3) and flowmeter (4) on the pipeline between salt thickener (1) and salt melting pond (2) respectively, the salt thick liquid of salt thickener (1) bottom comprises pure salt thick liquid and mother liquor, the mother liquor includes sodium chloride, sodium sulfate and water, sodium sulfate mass concentration is less than 7.4g/l in salt melting pond (2).
2. The novel vacuum salt making and discharging process according to claim 1, characterized in that: the pure salt slurry: volume ratio of mother liquor is 66%:34%, and the pulp density is a, and a =1.85 t/m.
3. The novel vacuum salt making and discharging process according to claim 2, characterized in that: the sodium chloride mass concentration is b, the sodium sulfate mass concentration is c, b =290g/l-300g/l, c =18 g/l-24g/l, the sodium chloride mass concentration in the salt dissolving pool (2) is d, and d =290g/l-310 g/l.
4. The novel vacuum salt making and discharging process according to claim 3, characterized in that: the sodium sulfate mass concentration calculation formula in the salt dissolving tank (2) is as follows:
1 t/m³=1000 g/L；
in the salt thickener (1), the calculation formula of sodium chloride in each cubic salt slurry is as follows:
E=66%*a+34%*b；
in the salt thickener (1), the calculation formula of sodium sulfate in each cubic salt slurry is as follows:
F=34%*c；
the calculation formula of water demand under d mass concentration after the salt dissolving pool (2) neutralizes salt water is as follows:
G=E/d-0.34；
the theoretical sodium sulfate content calculation formula after the salt dissolving pool (2) neutralizes salt water is as follows:
H= F/G。
5. the novel vacuum salt production and salt discharge process according to claim 4, wherein:
performing a full harvest under a =1.85t/m, b =290g/l, c =20g/l, d =300g/l, wherein the theoretical sodium sulfate content after neutralization of the salt pond (2) to brine is:
each cubic salt slurry contains sodium chloride: e = 66%. 1.85+ 34%. 0.29=1.32 t;
sodium sulfate per cubic salt slurry: f =34% + 0.02=0.0068 t;
water requirement for 300g/l of saline water: (iii) thin film obtained by ethanol harvest at G =1.32/0.3-0.34=4.06 m;
theoretical sodium sulfate content after conversion to brine:
h =0.0068/4.06=0.00167 tonnes/m cultivation =1.67 g/l.
6. The novel vacuum salt making and discharging process according to claim 5, characterized in that: the H is less than 7.4 g/l.
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Citations (6)
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|---|---|---|---|---|
| US4528168A (en) * | 1983-10-14 | 1985-07-09 | The Dow Chemical Company | Brine saturator method of operation |
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-
2020
- 2020-12-15 CN CN202011473452.3A patent/CN112897551A/en active Pending
Patent Citations (6)
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|---|---|---|---|---|
| US4528168A (en) * | 1983-10-14 | 1985-07-09 | The Dow Chemical Company | Brine saturator method of operation |
| CN2110512U (en) * | 1991-12-19 | 1992-07-22 | 自贡市轻工业设计研究院 | Charging machine for thickening salt pulp |
| CN102275953A (en) * | 2011-07-19 | 2011-12-14 | 湖北双环科技股份有限公司 | Method for producing caustic soda by purified brine |
| CN104477944A (en) * | 2014-11-20 | 2015-04-01 | 余春华 | Process of preparing anhydrous sodium sulfate from dilute brine in chlor-alkali industry |
| CN104628016A (en) * | 2015-01-29 | 2015-05-20 | 中盐金坛盐化有限责任公司 | High-nitrate mother solution nitrate coproduction apparatus and technique |
| CN109437244A (en) * | 2018-12-05 | 2019-03-08 | 安徽华塑股份有限公司 | The method of the calcium and magnesium salt slurry perfusion molten chamber of halogen well |
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| Title |
|---|
| 王海元等: "盐浆增稠设备的比较和选用", 《中国井矿盐》 * |
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Application publication date: 20210604 |
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