CN111732105A - Calcium fluosilicate production process - Google Patents
Calcium fluosilicate production process Download PDFInfo
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- CN111732105A CN111732105A CN202010725911.6A CN202010725911A CN111732105A CN 111732105 A CN111732105 A CN 111732105A CN 202010725911 A CN202010725911 A CN 202010725911A CN 111732105 A CN111732105 A CN 111732105A
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 26
- 239000011575 calcium Substances 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 80
- 238000003756 stirring Methods 0.000 claims abstract description 58
- 239000013078 crystal Substances 0.000 claims abstract description 37
- 239000002994 raw material Substances 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 46
- 238000003825 pressing Methods 0.000 claims description 25
- 238000000034 method Methods 0.000 claims description 23
- 238000001035 drying Methods 0.000 claims description 18
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 16
- 239000002253 acid Substances 0.000 claims description 14
- 239000000047 product Substances 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 10
- 230000035484 reaction time Effects 0.000 claims description 9
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 8
- 239000000920 calcium hydroxide Substances 0.000 claims description 8
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 8
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 8
- 239000000292 calcium oxide Substances 0.000 claims description 8
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 239000004744 fabric Substances 0.000 claims description 5
- 239000000706 filtrate Substances 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 3
- 238000004806 packaging method and process Methods 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 2
- 238000007599 discharging Methods 0.000 abstract description 8
- 239000007788 liquid Substances 0.000 description 7
- 206010044565 Tremor Diseases 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 2
- 229910001634 calcium fluoride Inorganic materials 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- -1 Calcium fluorosilicate Chemical compound 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Classifications
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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
- C01B33/00—Silicon; Compounds thereof
- C01B33/08—Compounds containing halogen
- C01B33/10—Compounds containing silicon, fluorine, and other elements
- C01B33/103—Fluosilicic acid; Salts thereof
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a calcium fluosilicate production process, wherein a first stirring paddle and a first rotating shaft are arranged in a reaction tank, the first rotating shaft is provided with the stirring paddle and is connected with a first driving motor, the lower part of the reaction tank is connected with a first conveying pipe, the first conveying pipe is connected with a filter press, a tank body at the bottom of the filter press is connected with a second conveying pipe, the second conveying pipe is connected with a negative pressure evaporator, the negative pressure evaporator is connected with a steam discharge pipe, the lower part of the negative pressure evaporator is connected with a crystal discharge pipe, the crystal discharge pipe is connected with a centrifugal dehydrator, the centrifugal dehydrator is connected with a third conveying pipe, the third conveying pipe is connected with a cyclone drier, and the; the first conveying pipe, the second conveying pipe, the steam discharging pipe, the crystal discharging pipe, the third conveying pipe and the discharging pipe are all provided with first control valves. Realizes low cost of raw materials for producing calcium fluosilicate, short operation time and convenient operation, and improves the production yield of products.
Description
Technical Field
The invention relates to the technical field of calcium fluosilicate production, and particularly relates to a production process of calcium fluosilicate.
Background
Calcium fluorosilicate is a chemical used as floatation agent, pesticide, etc. Appearance and properties: white crystalline powder. Relative density (water = 1): 2.66(17.5 ℃) solubility: is insoluble in water.
When the calcium fluosilicate is prepared, the quality of the prepared calcium fluosilicate is influenced by the selection of production raw materials and processes and the control of process conditions. Therefore, a production process of calcium fluosilicate is provided.
Disclosure of Invention
The invention aims to provide a production process of calcium fluosilicate, which realizes low cost of raw materials for producing the calcium fluosilicate, short operation time and convenient operation and improves the production yield of products.
In order to solve the technical problems, the invention adopts the following technical scheme:
a calcium fluosilicate production device comprises: the device comprises a reaction tank, a first stirring paddle, a first driving motor, a first conveying pipe, a filter press, a second conveying pipe, a negative pressure evaporator, a steam discharge pipe, a crystal discharge pipe, a centrifugal dehydrator, a third conveying pipe, a cyclone dryer, a discharge pipe and a first control valve;
a first stirring paddle is arranged in the reaction tank, a first rotating shaft is arranged on the first rotating shaft, the stirring paddle is connected with a first driving motor, the lower portion of the reaction tank is connected with a first conveying pipe, the first conveying pipe is connected with a filter press, a tank body at the bottom of the filter press is connected with a second conveying pipe, the second conveying pipe is connected with a negative pressure evaporator, the negative pressure evaporator is connected with a steam discharge pipe, the lower portion of the negative pressure evaporator is connected with a crystal discharge pipe, the crystal discharge pipe is connected with a centrifugal dehydrator, the centrifugal dehydrator is connected with a third conveying pipe, the third conveying pipe is connected with a cyclone dryer, and the cyclone;
the first conveying pipe, the second conveying pipe, the steam discharging pipe, the crystal discharging pipe, the third conveying pipe and the discharging pipe are all provided with first control valves.
Further, the method comprises the following steps of; be provided with first three-way valve on the first conveyer pipe, first conveyer pipe sets up through first three-way valve and feed liquor pipe intercommunication, feed liquor union coupling stirred tank, be provided with the second pivot in the stirred tank, be provided with the stirring rake in the second pivot, the second pivot is connected with second driving motor, the inlet tube is connected to the stirred tank, stirred tank one side connection circulating pipe is provided with the water pump on the circulating pipe, circulating pipe one end is provided with the second three-way valve, the circulating pipe passes through the second three-way valve and the setting of inlet tube intercommunication.
Further, the method comprises the following steps of; pH on-line detectors are arranged in the reaction tank and the stirring tank;
a baume degree tester is arranged in the negative pressure evaporator,
a temperature sensor is arranged in the cyclone dryer.
Further, the method comprises the following steps of; the method comprises the following steps:
raw material A: selecting one of calcium carbonate, calcium oxide and calcium hydroxide to react with fluosilicic acid and putting the mixture into a reaction tank for reaction;
b, a production process flow: the first stirring paddle is used for stirring and reacting the reaction tank, the pH value in the reaction tank is monitored by the pH online detector, a reaction solution in the reaction tank enters the filter press through the first conveying pipe, filtrate subjected to filter pressing by the filter press is subjected to negative pressure evaporation through the negative pressure evaporator to generate a water-containing crystal, the water-containing crystal enters the negative pressure evaporator through the second conveying pipe, water vapor in the negative pressure evaporator is discharged through the steam discharge pipe, the water-containing crystal in the negative pressure evaporator is subjected to cyclone drying after moisture in the water-containing crystal is reduced, and a product subjected to cyclone drying is subjected to moisture content detection;
c, collecting: and packaging the detected product.
Further, the method comprises the following steps of; in the step A, calcium carbonate, calcium oxide and calcium hydroxide are not powdered during reaction.
Further, the method comprises the following steps of; and in the step B, shaking down the filter residue after filter pressing by the filter press from the filter cloth of the filter press, enabling the shaken filter residue to enter into the stirring tank, feeding water into the stirring tank through the water inlet pipe, adding lime slurry into the stirring tank, monitoring the pH value in the stirring tank by the pH online detector, stirring by a second stirring paddle in the stirring tank, carrying out filter pressing by the filter press, and enabling the filter-pressed water to enter into the stirring tank through the circulating pipe.
Further, the method comprises the following steps of; and in the step B, the solution in the negative pressure evaporator is subjected to baume degree tester to detect the baume degree.
Further, the method comprises the following steps of; in the step B, the reaction time of the cyclone dryer is 1-4min, a temperature sensor detects the reaction temperature in the cyclone dryer, and the reaction temperature is lower than 80 ℃.
Further, the method comprises the following steps of; and in the step B, detecting the water content of the product subjected to cyclone drying, wherein the water content of the crystal is less than 0.5%.
Further, the method comprises the following steps of; in the step B, the pH in the reaction tank is = 4-6;
the pH in the stirred tank is greater than 8.
Compared with the prior art, the invention has at least one of the following beneficial effects:
1. realizes low cost of raw materials for producing calcium fluosilicate, short operation time and convenient operation, and improves the production yield of products.
2. The control of the acid environment in the reaction environment of the reaction tank is convenient for the reaction, the solid-liquid reaction is realized, no water is added, the generation of by-products is reduced, and the evaporated water is less.
3. Washing the filter residue with water, adding water and then adding lime slurry, wherein the filter residue after filter pressing of the filter press meets the requirement of common solid wastes, and the environmental hazard is reduced.
Drawings
FIG. 1 is a schematic view of the structure of the present invention.
In the figure: reaction tank (1), first stirring rake (2), first driving motor (3), first conveyer pipe (4), pressure filter (5), second conveyer pipe (6), negative pressure evaporator (7), steam discharging pipe (8), crystal discharging pipe (9), centrifugal dehydrator (10), third conveyer pipe (11), cyclone drier (12), row material pipe (13), first control valve (14), first three-way valve (15), feed liquor pipe (16), stirred tank (17), second stirring rake (18), second driving motor (19), inlet tube (20), circulating pipe (21), water pump (22), second three-way valve (23), pH on-line detector (24), baume degree tester (25), temperature sensor (26), first pivot (27), second pivot (28).
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings and embodiments, as shown in fig. 1. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1:
a calcium fluosilicate production device comprises: the device comprises a reaction tank 1, a first stirring paddle 2, a first driving motor 3, a first conveying pipe 4, a filter press 5, a second conveying pipe 6, a negative pressure evaporator 7, a steam discharge pipe 8, a crystal discharge pipe 9, a centrifugal dehydrator 10, a third conveying pipe 11, a cyclone dryer 12, a discharge pipe 13 and a first control valve 14;
a first stirring paddle 2 and a first rotating shaft 27 are arranged in the reaction tank 1, the stirring paddle 2 arranged on the first rotating shaft 27 is connected with a first driving motor 3, the lower part of the reaction tank 1 is connected with a first conveying pipe 4, the first conveying pipe 4 is connected with a filter press 5, a tank body at the bottom of the filter press 5 is connected with a second conveying pipe 6, the second conveying pipe 6 is connected with a negative pressure evaporator 7, the negative pressure evaporator 7 is connected with a steam discharge pipe 8, the lower part of the negative pressure evaporator 7 is connected with a crystal discharge pipe 9, the crystal discharge pipe 9 is connected with a centrifugal dehydrator 10, the centrifugal dehydrator 10 is connected with a third conveying pipe 11, the third conveying pipe 11 is connected with a cyclone drier 12, and the cyclone drier;
the first conveying pipe 4, the second conveying pipe 6, the steam discharge pipe 8, the crystal discharge pipe 9, the third conveying pipe 11 and the discharge pipe 13 are all provided with a first control valve 14; the raw materials of calcium fluosilicate are stirred and reacted in the reaction tank 1 through the first stirring paddle 2, the solution after reaction enters the filter press 5 for filter pressing, the liquid generated by filter pressing enters the negative pressure evaporator 7 for negative pressure evaporation, the steam is discharged through the steam discharge pipe 8, the water-containing crystal evaporated by negative pressure enters the centrifugal dehydrator 10 through the crystal discharge pipe 9 for centrifugal dehydration, and after dehydration, the cyclone drier 12 performs cyclone drying.
Example 2:
on the basis of embodiment 1, a first three-way valve 15 is arranged on a first conveying pipe 4, the first conveying pipe 4 is communicated with a liquid inlet pipe 16 through the first three-way valve 15, the liquid inlet pipe 16 is connected with a stirring tank 17, a second rotating shaft 28 is arranged in the stirring tank 17, a stirring paddle 18 is arranged on the second rotating shaft 28, the second rotating shaft 28 is connected with a second driving motor 19, the stirring tank 17 is connected with a water inlet pipe 20, one side of the stirring tank 17 is connected with a circulating pipe 21, a water pump 22 is arranged on the circulating pipe 21, a second three-way valve 23 is arranged at one end of the circulating pipe 21, and the circulating pipe 21 is communicated with the water inlet pipe 20; the solution after the reaction enters into the pressure filter 5 to carry out the filter-pressing, the filter residue that the filter-pressing produced is trembled down on by the filter cloth of pressure filter 5, the filter residue that trembles down enters into stirred tank 17, it intakes through inlet tube 20 in the stirred tank 17, add the lime mud again and enter into stirred tank 17, the pH value in the control stirred tank 17, reentrant pressure filter 5 carries out the filter-pressing, the water of filter-pressing enters into stirred tank 17 through circulating pipe 21, can cyclic utilization, the filter residue that pressure produced can tremble down the emission, the filter residue that trembles down is general discarded object, the processing of being convenient.
Example 3:
on the basis of the embodiment 1-2, pH on-line detectors 24 are arranged in the reaction tank 1 and the stirring tank 17;
a baume degree tester 25 is arranged in the negative pressure evaporator 7,
a temperature sensor 26 is arranged in the cyclone dryer 12; can monitor pH, Baume degree and temperature.
Example 4:
on the basis of the embodiments 1-3, the method comprises the following steps:
raw material A: one of calcium carbonate, calcium oxide and calcium hydroxide is selected to react with fluosilicic acid and then is put into a reaction tank 1 for reaction;
b, a production process flow: the first stirring paddle 2 is used for stirring and reacting the reaction tank 1, the pH value in the reaction tank 1 is monitored by a pH online detector 24, a reaction solution in the reaction tank 1 enters a filter press 5 through a first conveying pipe 4, filtrate subjected to filter pressing by the filter press 5 is subjected to negative pressure evaporation through a negative pressure evaporator 7 to generate a water-containing crystal, the water-containing crystal enters the negative pressure evaporator 7 through a second conveying pipe 6, water vapor in the negative pressure evaporator 7 is discharged through a vapor discharge pipe 8, the water-containing crystal in the negative pressure evaporator 7 is subjected to moisture reduction and then enters a cyclone drier 12 for cyclone drying, and the water content of a product subjected to cyclone drying is detected;
c, collecting: packaging the detected product;
selecting one of calcium carbonate, calcium oxide and calcium hydroxide to react with fluosilicic acid and then putting the selected one into a reaction tank 1 for reaction, a first stirring paddle 2 is used for stirring reaction, the fluosilicic acid in the reaction raw materials is slightly excessive, so that the reaction environment is acidic, byproducts such as calcium fluoride and the like can be generated in an alkaline environment, the calcium fluoride emission can pollute the environment, the reaction is directly carried out by selecting one of solid raw materials of calcium carbonate, calcium oxide and calcium hydroxide and a liquid raw material of fluosilicic acid, no water is added, the evaporation of heat and moisture generated in the reaction is less, the solution after the reaction enters a filter press 5 through a first conveying pipe 4, the filter press 5 is used for filter pressing, the generated filtrate enters a negative pressure evaporator 7 for negative pressure evaporation to generate a hydrous crystal, the hydrous crystal is centrifugally dehydrated through a centrifugal dehydrator 10 to reduce the moisture content of the hydrous crystal, and is subjected to cyclone drying through a cyclone dryer 12, the product after cyclone drying is subjected to water content detection and then is packaged, the reaction time in the whole process is short, the cost of raw materials is low, the operation is convenient,
example 5:
in step A, calcium carbonate, calcium oxide and calcium hydroxide are not powdered when they are reacted, based on examples 1 to 4; the powder enters to be convenient for solid-liquid reaction with the fluosilicic acid.
Example 6:
on the basis of the embodiments 1 to 5, in the step B, filter residue after filter pressing of the filter press 5 is shaken off from the filter cloth of the filter press 5, the shaken filter residue enters the stirring tank 17, water enters the stirring tank 17 through the water inlet pipe 20, then lime slurry is added to enter the stirring tank 17, the pH value in the stirring tank 17 is monitored by the online pH detector 24, the second stirring paddle 18 in the stirring tank 17 is used for stirring, the filter press 5 performs filter pressing, and the filter-pressed water enters the stirring tank 17 through the circulating pipe 21; solution after the reaction enters into pressure filter 5 and carries out the filter-pressing, the filter residue that the filter-pressing produced is trembled down on by pressure filter 5's the filter cloth, the filter residue that trembles down enters into stirred tank 17, it intakes through inlet tube 20 in the stirred tank 17, add lime thick liquid during washing and enter into stirred tank 17 in, the pH value in the control stirred tank 17, reentrant pressure filter 5 carries out the filter-pressing, the water of filter-pressing enters into stirred tank 17 through circulating pipe 21, can cyclic utilization, the filter residue that pressure produced can tremble down the emission, the filter residue that trembles down is general discarded object, the processing of being convenient for.
Example 7:
on the basis of the examples 1 to 6, in the step B, the solution in the negative pressure evaporator 7 is subjected to a baume degree tester 25 to detect the baume degree; the baume degree tester 25 detects the baume degree in the negative pressure evaporator 7, and the baume degree is 40-50, so that the requirement is met.
Example 8:
on the basis of the examples 1 to 7, in the step B, the reaction time of the cyclone dryer 12 is 1min, the temperature sensor 26 detects the reaction temperature in the cyclone dryer 12, and the reaction temperature is lower than 80 ℃; the reaction temperature is higher than 80 ℃, byproducts are generated at high temperature, and the control of the reaction time is convenient for cyclone drying and is beneficial to dehydrating and drying the crystal.
Example 9:
on the basis of the examples 1 to 8, in the step B, the reaction time of the cyclone dryer 12 is 4min, the temperature sensor 26 detects the reaction temperature in the cyclone dryer 12, and the reaction temperature is lower than 80 ℃; the reaction temperature is higher than 80 ℃, byproducts are generated at high temperature, and the control of the reaction time is convenient for cyclone drying and is beneficial to dehydrating and drying the crystal.
Example 10:
on the basis of examples 1 to 9, in step B, the reaction time of the cyclone dryer 12 is 2.5min, and the temperature sensor 26 detects the reaction temperature in the cyclone dryer 12, wherein the reaction temperature is lower than 80 ℃; the reaction temperature is higher than 80 ℃, byproducts are generated at high temperature, and the control of the reaction time is convenient for cyclone drying and is beneficial to dehydrating and drying the crystal.
Example 9:
on the basis of the embodiments 1 to 3, in the step B, the water content of the product after cyclone drying is detected, and the water content of the crystal is less than 0.5 percent; the quality of the product is convenient to improve.
Example 10:
in the step B, the pH =4 to 6 in the reaction tank 1 is set to be lower than that in examples 1 to 9;
the pH value in the stirring tank 17 is more than 8; the control of acid value in the reaction tank is convenient for carry out the reaction in the reaction tank, and the control of acid value in the stirred tank 17 makes the filter residue be convenient for wash, and the filter residue satisfies the requirement of general solid waste after 5 filter pressing of pressure filter.
Example 11:
on the basis of examples 1 to 10, in the step B, the pH =4 to 6 in the reaction tank 1;
the pH value in the stirring tank 17 is more than 8; the control of acid value in the reaction tank is convenient for carry out the reaction in the reaction tank, and the control of acid value in the stirred tank 17 makes the filter residue be convenient for wash, and the filter residue satisfies the requirement of general solid waste after 5 filter pressing of pressure filter.
Example 12:
in the step B, the pH =4 to 6 in the reaction tank 1 is set to be lower than that in examples 1 to 11;
the pH value in the stirring tank 17 is more than 8; the control of acid value in the reaction tank is convenient for carry out the reaction in the reaction tank, and the control of acid value in the stirred tank 17 makes the filter residue be convenient for wash, and the filter residue satisfies the requirement of general solid waste after 5 filter pressing of pressure filter.
Although the invention has been described herein with reference to a number of illustrative embodiments thereof, it should be understood that numerous other modifications and embodiments can be devised by those skilled in the art that will fall within the spirit and scope of the principles of this disclosure. More specifically, various variations and modifications are possible in the component parts and/or arrangements of the subject combination arrangement within the scope of the disclosure, the drawings and the appended claims. In addition to variations and modifications in the component parts and/or arrangements, other uses will also be apparent to those skilled in the art.
Claims (10)
1. The utility model provides a calcium fluosilicate apparatus for producing which characterized in that: the method comprises the following steps: the device comprises a reaction tank (1), a first stirring paddle (2), a first driving motor (3), a first conveying pipe (4), a filter press (5), a second conveying pipe (6), a negative pressure evaporator (7), a steam discharge pipe (8), a crystal discharge pipe (9), a centrifugal dehydrator (10), a third conveying pipe (11), a cyclone dryer (12), a discharge pipe (13) and a first control valve (14);
a first rotating shaft (27) is arranged in the reaction tank (1), a stirring paddle (2) is arranged on the first rotating shaft (27), the first stirring paddle (2) is connected with a first driving motor (3), a first conveying pipe (4) is connected to the lower portion of the reaction tank (1), the first conveying pipe (4) is connected with a filter press (5), a second conveying pipe (6) is connected to a tank body at the bottom of the filter press (5), a negative pressure evaporator (7) is connected to the second conveying pipe (6), the negative pressure evaporator (7) is connected to a steam discharge pipe (8), a crystal discharge pipe (9) is connected to the lower portion of the negative pressure evaporator (7), the crystal discharge pipe (9) is connected with a centrifugal dehydrator (10), the centrifugal dehydrator (10) is connected with a third conveying pipe (11), the third conveying pipe (11) is connected with a cyclone dryer (12), and the cyclone dryer (12) is connected;
the first conveying pipe (4), the second conveying pipe (6), the steam discharge pipe (8), the crystal discharge pipe (9), the third conveying pipe (11) and the discharge pipe (13) are all provided with a first control valve (14).
2. The calcium fluosilicate production device of claim 1, wherein: be provided with first three-way valve (15) on first conveyer pipe (4), first conveyer pipe (4) set up through first three-way valve (15) and feed liquor pipe (16) intercommunication, agitator tank (17) are connected in feed liquor pipe (16), be provided with second pivot (28) in agitator tank (17), be provided with stirring rake (18) on second pivot (28), second pivot (28) are connected with second driving motor (19), inlet tube (20) are connected in agitator tank (17), circulating pipe (21) is connected to agitator tank (17) one side, be provided with water pump (22) on circulating pipe (21), circulating pipe (21) one end is provided with second three-way valve (23), circulating pipe (21) set up through second three-way valve (23) and inlet tube (20) intercommunication.
3. The calcium fluosilicate production device of claim 1, wherein: pH on-line detectors (24) are arranged in the reaction tank (1) and the stirring tank (17);
a Baume degree tester (25) is arranged in the negative pressure evaporator (7),
a temperature sensor (26) is arranged in the cyclone dryer (12).
4. A process for producing a calcium silicofluoride plant using the calcium silicofluoride according to any one of claims 1 to 3, characterized in that: the method comprises the following steps:
raw material A: one of calcium carbonate, calcium oxide and calcium hydroxide is selected to react with fluosilicic acid and then put into a reaction tank (1) for reaction;
b, a production process flow: a first stirring paddle (2) is used for stirring reaction in a reaction tank (1), a pH value in the reaction tank (1) is monitored by a pH online detector (24), a reaction solution in the reaction tank (1) enters a filter press (5) through a first conveying pipe (4), filtrate subjected to filter pressing by the filter press (5) is subjected to negative pressure evaporation through a negative pressure evaporator (7) to generate a water-containing crystal, the water-containing crystal enters the negative pressure evaporator (7) through a second conveying pipe (6), water vapor in the negative pressure evaporator (7) is discharged through a vapor discharge pipe (8), the water-containing crystal in the negative pressure evaporator (7) is subjected to moisture reduction and then enters a cyclone dryer (12) for cyclone drying, and a product subjected to cyclone drying is subjected to moisture content detection;
c, collecting: and packaging the detected product.
5. The process for producing calcium fluosilicate according to claim 4, wherein: in the step A, calcium carbonate, calcium oxide and calcium hydroxide are not powdered during reaction.
6. The process for producing calcium fluosilicate according to claim 4, wherein: in the step B, filter residue after filter pressing of the filter press (5) is shaken down on the filter cloth of the filter press (5), the filter residue that is shaken down enters into the stirring tank (17), water enters into the stirring tank (17) through the water inlet pipe (20), lime slurry is added into the stirring tank (17), the pH value in the stirring tank (17) is monitored by the pH online detector (24), the second stirring paddle (18) is stirred in the stirring tank (17), the filter press (5) carries out filter pressing, and the water of filter pressing enters into the stirring tank (17) through the circulating pipe (21).
7. The process for producing calcium fluosilicate according to claim 4, wherein: and in the step B, the solution in the negative pressure evaporator (7) is subjected to baume degree testing by a baume degree tester (25).
8. The process for producing calcium fluosilicate according to claim 4, wherein: in the step B, the reaction time of the cyclone dryer (12) is 1-4min, and the temperature sensor (26) detects the reaction temperature in the cyclone dryer (12), wherein the reaction temperature is lower than 80 ℃.
9. The process for producing calcium fluosilicate according to claim 4, wherein: and in the step B, detecting the water content of the product subjected to cyclone drying, wherein the water content of the crystal is less than 0.5%.
10. The process for producing calcium fluosilicate according to claim 4, wherein: in the step B, the pH in the reaction tank (1) is = 4-6;
the pH in the stirred tank (17) is greater than 8.
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| CN202010725911.6A CN111732105A (en) | 2020-07-24 | 2020-07-24 | Calcium fluosilicate production process |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS577812A (en) * | 1980-06-13 | 1982-01-16 | Nippon Mining Co Ltd | Removing method for fluorine from waste sulfuric acid |
| CN86105595A (en) * | 1985-07-26 | 1987-01-21 | 皮奇尼铝业公司 | Produce the production method of the raw material calcium silicofluoride of Calcium Fluoride (Fluorspan) and pure fluosilicic acid |
| CN102092719A (en) * | 2011-01-14 | 2011-06-15 | 云南常青树化工有限公司 | Method for producing industrial calcium fluosilicate |
| CN102701250A (en) * | 2012-06-29 | 2012-10-03 | 怀化市骏源精细化工有限公司 | Method and device for treating aluminium polychlorid reaction residues |
| CN204824189U (en) * | 2015-08-11 | 2015-12-02 | 湖北三雄科技发展有限公司 | Utilize processing apparatus of fluoride waste production calcium fluosilicate |
| CN210885327U (en) * | 2019-09-19 | 2020-06-30 | 昆明合起工贸有限公司 | Magnesium fluosilicate preparation system |
-
2020
- 2020-07-24 CN CN202010725911.6A patent/CN111732105A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS577812A (en) * | 1980-06-13 | 1982-01-16 | Nippon Mining Co Ltd | Removing method for fluorine from waste sulfuric acid |
| CN86105595A (en) * | 1985-07-26 | 1987-01-21 | 皮奇尼铝业公司 | Produce the production method of the raw material calcium silicofluoride of Calcium Fluoride (Fluorspan) and pure fluosilicic acid |
| CN102092719A (en) * | 2011-01-14 | 2011-06-15 | 云南常青树化工有限公司 | Method for producing industrial calcium fluosilicate |
| CN102701250A (en) * | 2012-06-29 | 2012-10-03 | 怀化市骏源精细化工有限公司 | Method and device for treating aluminium polychlorid reaction residues |
| CN204824189U (en) * | 2015-08-11 | 2015-12-02 | 湖北三雄科技发展有限公司 | Utilize processing apparatus of fluoride waste production calcium fluosilicate |
| CN210885327U (en) * | 2019-09-19 | 2020-06-30 | 昆明合起工贸有限公司 | Magnesium fluosilicate preparation system |
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Application publication date: 20201002 |