CN209039069U - Acidic silicasol production system - Google Patents
Acidic silicasol production system Download PDFInfo
- Publication number
- CN209039069U CN209039069U CN201821675916.7U CN201821675916U CN209039069U CN 209039069 U CN209039069 U CN 209039069U CN 201821675916 U CN201821675916 U CN 201821675916U CN 209039069 U CN209039069 U CN 209039069U
- Authority
- CN
- China
- Prior art keywords
- tank
- pipeline
- crystallization apparatus
- heat exchanger
- heating tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Silicon Compounds (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model relates to a kind of acidic silicasol production systems, first reaction kettle passes through pipeline and cationic swap tank, the connection of active silicic acid temporary storage tank, the active silicic acid temporary storage tank passes through pipeline and the first heating tank respectively, second heating tank, the connection of third heating tank, first heating tank, second heating tank, third heating tank is sequentially communicated by pipeline, the third heating tank discharge port is connected to by pipeline with cationic swap tank feeding inlet, the cation swap tank discharge port also passes through pipeline and concentration tank, first filter device is sequentially communicated, the cation swap tank is equipped with the first ionized water and is passed through pipeline, diluted acid access tube, the cation swap tank is connected to by pipeline with waste water treatment tank.Big, the with high purity acidic silicasol product of the silica solution granularity that the utility model is prepared, period are suitable for that stability is optimal, are suitble to produce in enormous quantities.
Description
Technical field
The utility model belongs to silica solution production technical field, is related to for acidic silicasol production system.
Background technique
Silica solution be the colloidal solution that the colloidal particles of silica are dispersed in water also known as silica sol, polysilicon acid,
Or silica hydrosol.Since silicon dioxide granule has biggish surface-active in silica solution, by the modified energy again in surface
It is miscible with organic polymer, therefore be widely used in organic and inorganic material adhesive, it is applied to coating, accurate casting
It makes, the industries such as refractory material and electronics industry.Every year, consume a large amount of foreign exchange high price import in China, and China oneself produces
Silica solution there is also unsalable phenomenons sometimes.Therefore serial silica solution product and exploitation silica solution new application are developed
It has great significance.
Summary of the invention
In order to solve the above technical problems, the utility model provides a kind of acidic silicasol production system, the purity is high of production,
Its waste water is recycled.
The embodiment of the utility model is:
A kind of acidic silicasol production system, first reaction kettle pass through pipeline and cationic swap tank, active silicic acid
Temporary storage tank connection, the active silicic acid temporary storage tank pass through respectively pipeline and the first heating tank, the second heating tank, third heating tank according to
Secondary connection, first heating tank, the second heating tank and third heating tank are sequentially communicated by pipeline, and the third heating tank goes out
Material mouth is connected to by pipeline with cationic swap tank feeding inlet, and the cation swap tank discharge port also passes through pipeline and concentration
Tank, the first filter device are sequentially communicated, and the cation swap tank is equipped with the first ionized water and is passed through pipeline and diluted acid access tube, institute
Cationic swap tank is stated to be connected to by pipeline with waste water treatment tank.
Preferably, first heating tank, the second heating tank and third heating tank are from top to bottom sequentially communicated by pipeline,
Agitating shaft is equipped with inside first heating tank, the agitating shaft is hollow structure and passes through pipeline and active silicic acid temporary storage tank
Connection, the agitating shaft surface are equipped with discharge hole, and the agitating shaft is equipped with spiral helicine stirring blade, in the stirring blade
Portion is equipped with resistance wire, and the agitating shaft passes through the motor driven being arranged in outside the first heating tank.
It is further preferred that the stirring shaft cross section is circular cylinder, the cross-sectional diameter of the agitating shaft along
Direction far from motor successively reduces.
Preferably, the waste water treatment tank and preheating can, First Heat Exchanger, the first crystallization apparatus, the first concentration flow container, the
Two heat exchangers, the second crystallization apparatus, the second concentration flow container, third heat exchanger, third crystallization apparatus, the second device for filtering and collecting are logical
Piping is sequentially communicated.
It is further preferred that first crystallization apparatus, the second crystallization apparatus, third crystallization apparatus are from top to bottom equipped with steaming
Hair room and crystallisation chamber, the First Heat Exchanger are connected to the vaporization chamber of the first crystallization apparatus, the crystallization of first crystallization apparatus
Room is connected to the first concentration flow container, and second heat exchanger is connected to the vaporization chamber of the second crystallization apparatus, the second crystallization dress
The crystallisation chamber set is connected to the second concentration flow container, and the third heat exchanger is connected to the vaporization chamber of third crystallization apparatus, and described the
The crystallisation chamber of three crystallization apparatus is connected to the second device for filtering and collecting.
It is further preferred that the vaporization chamber of first crystallization apparatus connects through the first vacuum pressure pump and the second heat exchanger
Logical, the vaporization chamber of second crystallization apparatus is connected to through the second vacuum pressure pump with third heat exchanger, the steaming of third crystallization apparatus
Hair room is connected to through third vacuum pressure pump with First Heat Exchanger.
It is further preferred that the First Heat Exchanger, the second heat exchanger, third heat exchanger are respectively equipped with condensation water collection
Tank.
Preferably, first filter device is connected to acidic silicasol product handling system tank, the acidic silicasol finished product
Process tank is equipped with stabilizer feeding inlet.
The utility model the utility model has the advantages that
1. the silica solution granularity that the utility model is prepared is big, the acidic silicasol product of purity is high, the period is suitable, surely
It is qualitative optimal, it is suitble to produce in enormous quantities.
2. obtaining the acidic silicasol product that granularity is big, with high purity by being continuously concentrated by evaporation;Secondly because acid silicon
The light base in colloidal sol colloidal grain surface part is replaced by organic group, increases the steric hindrance between particle, so that metastable
The acidic silicasol solution of state becomes more stable.
3. the waste water that cationic swap tank generates carries out acid-base neutralization processing in waste water treatment tank, do not need to be added other
Clean process, and easy to operate, cost for wastewater treatment is low.The sodium chloride solution that wastewater treatment obtains is by preheating can, the first heat exchange
Device, the first crystallization apparatus, first concentration flow container, the second heat exchanger, the second crystallization apparatus, second concentration flow container, third heat exchanger,
Third crystallization apparatus carries out the recovery processing of three-level condensing crystallizing.
4. the present invention reduces separate unit using the sodium chloride of the low concentration in the waste water of three-level concentration and crystallization device series connection recycling
The volume of equipment.The vaporization chamber of first crystallization apparatus is connected to through the first vacuum pressure pump with the second heat exchanger, and described second
The vaporization chamber of crystallization apparatus is connected to through the second vacuum pressure pump with third heat exchanger, and the vaporization chamber of third crystallization apparatus is true through third
Empty pressure pump is connected to First Heat Exchanger.Only need to provide Preheated steam for the first crystallization apparatus, energy conservation 70~90%, save at
This.
5. stabilizer is added, and (stabilizer is boron, and boron rubs with to acidic silicasol during acidic silicasol saves
You are than the stability for 0. 5 and raising silica solution.
6. being equipped with agitating shaft 31 inside first heating tank 3, the agitating shaft 31 is hollow structure and passes through pipeline
It is connected to active silicic acid temporary storage tank 203, the agitating shaft 31 is equipped with spiral helicine stirring blade 33, in the stirring blade 33
Portion is equipped with resistance wire, and the agitating shaft 31 passes through the motor 34 being arranged in outside the first heating tank 3 and drives, and guarantees the rate of heating
With the uniformity of heating, while 31 surface of the agitating shaft is equipped with discharge hole 32 and facilitates charging, and mixing effect can be improved.
Detailed description of the invention
Fig. 1 utility model device system schematic；
Fig. 2 utility model device structural schematic diagram；
Wherein: the first reaction kettle 1, cationic swap tank 2, the first ionized water are passed through pipeline 201, and diluted acid access tube 202 is living
Property silicic acid temporary storage tank 203, the first heating tank 3, agitating shaft 31, discharge hole 32, stirring blade 33, motor 34, the second heating tank 4,
Third heating tank 5, concentration tank 6, the first filter device 7, waste water treatment tank 8, preheating can 9, First Heat Exchanger 10, the first crystallization dress
Set 11, the first concentration flow container 12, the second heat exchanger 13, the second crystallization apparatus 14, the second concentration flow container 15, third heat exchanger 16,
Third crystallization apparatus 17, the second device for filtering and collecting 18, the first vacuum pressure pump 19, the second vacuum pressure pump 20, third vacuum
Pressure pump 21, acidic silicasol product handling system tank 22, stabilizer feeding inlet 221.
Specific embodiment
Further illustrate the utility model below with reference to embodiment, but the range of the requires of the utility model protection not office
It is limited to the range of embodiment statement.
Embodiment 1
Such as Fig. 1-2, a kind of acidic silicasol production system, first reaction kettle 1 passes through pipeline and cationic swap tank
2, active silicic acid temporary storage tank 203 is connected to, and the active silicic acid temporary storage tank 203 is added by pipeline and the first heating tank 3, second respectively
Hot tank 4, third heating tank 5 are connected to, and first heating tank 3, the second heating tank 4, third heating tank 5 are successively connected by pipeline
Logical, 5 discharge port of third heating tank is connected to by pipeline with cationic 2 feeding inlet of swap tank, and the cation swap tank 2 goes out
Material mouth also passes through pipeline and is sequentially communicated with concentration tank 6, the first filter device 7, and the cation swap tank 2 is equipped with the first ionized water
It is passed through pipeline 201, diluted acid access tube 202, the cation swap tank 2 is connected to by pipeline with waste water treatment tank 8.
Preferably, first heating tank 3, the second heating tank 4, third heating tank 5 are from top to bottom successively connected by pipeline
It is logical, agitating shaft 31 is equipped with inside first heating tank 3, the agitating shaft 31 is hollow structure and passes through pipeline and activated silica
Sour temporary storage tank 203 is connected to, and 31 surface of agitating shaft is equipped with discharge hole 32, and the agitating shaft 31 is equipped with spiral helicine paddle
Piece 33, resistance wire is equipped with inside the stirring blade 33, and the agitating shaft 31 passes through the motor being arranged in outside the first heating tank 3
34 drivings.
It is further preferred that 31 cross section of agitating shaft is circular cylinder, the cross-sectional diameter of the agitating shaft 31
It is successively reduced along the direction far from motor 34.
Preferably, the waste water treatment tank 8 is concentrated with preheating can 9, First Heat Exchanger 10, the first crystallization apparatus 11, first
Flow container 15, third heat exchanger 16, third crystallization apparatus is concentrated in flow container 12, the second heat exchanger 13, the second crystallization apparatus 14, second
17, the second device for filtering and collecting 18 is sequentially communicated by pipeline.
It is further preferred that first crystallization apparatus 11, the second crystallization apparatus 14, third crystallization apparatus 17 are from top to bottom
Equipped with vaporization chamber and crystallisation chamber, the First Heat Exchanger 10 is connected to the vaporization chamber of the first crystallization apparatus 11, first crystallization
The crystallisation chamber of device 11 is connected to the first concentration flow container 12, and the vaporization chamber of second heat exchanger 13 and the second crystallization apparatus 14 connects
Logical, the crystallisation chamber of second crystallization apparatus 14 is connected to the second concentration flow container 15, and the third heat exchanger 16 is crystallized with third
The vaporization chamber of device 17 is connected to, and the crystallisation chamber of the third crystallization apparatus 17 is connected to the second device for filtering and collecting 18.
It is further preferred that the vaporization chamber of first crystallization apparatus 11 is through the first vacuum pressure pump 19 and the second heat exchange
Device 13 is connected to, and the vaporization chamber of second crystallization apparatus 14 is connected to through the second vacuum pressure pump 20 with third heat exchanger 16, third
The vaporization chamber of crystallization apparatus 17 is connected to through third vacuum pressure pump 21 with First Heat Exchanger 10.
It is further preferred that the First Heat Exchanger 10, the second heat exchanger 13, third heat exchanger 16 are respectively equipped with condensation
Water collecting tank.
Preferably, first filter device 7 is connected to acidic silicasol product handling system tank 22, the acidic silicasol at
Product process tank 22 is equipped with stabilizer feeding inlet 221.
When the utility model is used: the waterglass after dilution being passed through into cationic swap tank 2 in the first reaction kettle 1 and is exchanged
Column removes sodium ion therein and other cations.Then, the active silicic acid solution point first flowed out from cationic swap tank 2
Heating tank 3, the second heating tank 4, third heating tank 5 are successively boiled, and during boiling, it is molten to each lead into active silicic acid
Liquid, treated, and modified silicasol activates yang again that ion exchange pot 2 obtains the acidic silicasol of pH=1.5, enters back into concentration tank
6 are concentrated by evaporation, and entering back into 7 impurity screening of the first filter device can be obtained acidic silicasol product.Cationic swap tank 2 regenerates
Make that many acid waste waters can be generated, sodium hydroxide is added in waste water treatment tank 8 and carries out being processed into neutral water, it is molten to obtain sodium chloride
Liquid, into preheating can 9, First Heat Exchanger 10, the first crystallization apparatus 10, the second heat exchanger 13, the second crystallization apparatus 14, third are changed
Hot device 16, third crystallization apparatus 17 carry out the crystallization concentration and recovery of thtee-stage shiplock.First filter device 7 and acidic silicasol
Product handling system tank 22 is connected to, and the acidic silicasol product handling system tank 22 is equipped with stabilizer feeding inlet 221.It is protected in acidic silicasol
During depositing, be added stabilizer described in stabilizer be boron, boron with to acidic silicasol molar ratio be 0. 5 and 1 raising silicon it is molten
The stability of glue.
Preferred embodiments of the present invention above described embodiment only expresses, the description thereof is more specific and detailed,
But it should not be understood as limiting the scope of the patent of the utility model.It should be pointed out that for the common of this field
For technical staff, without departing from the inventive concept of the premise, several deformations can also be made, improves and substitutes, these are all
Belong to the protection scope of the utility model.Therefore, the scope of protection shall be subject to the appended claims for the utility model patent.
Claims (7)
1. a kind of acidic silicasol production system, including the first reaction kettle (1), it is characterised in that: first reaction kettle (1) is logical
Piping is sequentially communicated with cationic swap tank (2), active silicic acid temporary storage tank (203), the active silicic acid temporary storage tank (203) point
Not Tong Guo pipeline be sequentially communicated with the first heating tank (3), the second heating tank (4), third heating tank (5), the first heating tank (3),
Second heating tank (4) and third heating tank (5) are sequentially communicated by pipeline, and third heating tank (5) discharge port passes through pipeline and sun
The connection of ion exchange pot (2) feeding inlet, described cation swap tank (2) discharge port also pass through pipeline and concentration tank (6), the first mistake
Filter device (7) is sequentially communicated, and the cation swap tank (2) is equipped with the first ionized water and is passed through pipeline (201) and diluted acid access tube
(202), the cationic swap tank (2) is connected to by pipeline with waste water treatment tank (8).
2. acidic silicasol production system according to claim 1, it is characterised in that: first heating tank (3), second
Heating tank (4), third heating tank (5) structure is the same and is from top to bottom sequentially communicated by pipeline, in first heating tank (3)
Portion is equipped with agitating shaft (31), and the agitating shaft (31) is hollow structure and is connected by pipeline and active silicic acid temporary storage tank (203)
Logical, agitating shaft (31) surface is equipped with discharge hole (32), and the agitating shaft (31) is equipped with spiral helicine stirring blade (33),
Resistance wire, the agitating shaft (31) electricity external in the first heating tank (3) by setting are equipped with inside the stirring blade (33)
Machine (34) driving.
3. acidic silicasol production system according to claim 2, it is characterised in that: the agitating shaft (31) is cross section
It is circular cylinder, the cross-sectional diameter of the agitating shaft (31) is successively reduced along the direction far from motor (34).
4. acidic silicasol production system according to claim 1, it is characterised in that: the waste water treatment tank (8) and pre-
Hot tank (9), First Heat Exchanger (10), the first crystallization apparatus (11), the first concentration flow container (12), the second heat exchanger (13), second
Dress is collected by filtration in crystallization apparatus (14), the second concentration flow container (15), third heat exchanger (16), third crystallization apparatus (17), second
(18) are set to be sequentially communicated by pipeline.
5. acidic silicasol production system according to claim 4, it is characterised in that: first crystallization apparatus (11),
Second crystallization apparatus (14), third crystallization apparatus (17) are from top to bottom equipped with vaporization chamber and crystallisation chamber, the First Heat Exchanger
(10) it is connected to the vaporization chamber of the first crystallization apparatus (11), the crystallisation chamber of first crystallization apparatus (11) and the first concentration flow container
(12) it is connected to, second heat exchanger (13) is connected to the vaporization chamber of the second crystallization apparatus (14), second crystallization apparatus
(14) crystallisation chamber is connected to the second concentration flow container (15), the evaporation of the third heat exchanger (16) and third crystallization apparatus (17)
Room connection, the crystallisation chamber of the third crystallization apparatus (17) are connected to the second device for filtering and collecting (18).
6. acidic silicasol production system according to claim 5, it is characterised in that: first crystallization apparatus (11)
Vaporization chamber is connected to through the first vacuum pressure pump (19) with the second heat exchanger (13), the vaporization chamber warp of second crystallization apparatus (14)
Second vacuum pressure pump (20) is connected to third heat exchanger (16), and the vaporization chamber of third crystallization apparatus (17) is through third vacuum pressure
Pump (21) is connected to First Heat Exchanger (10), the First Heat Exchanger (10), the second heat exchanger (13), third heat exchanger (16) point
It She You not condensation water collection tank.
7. acidic silicasol production system according to claim 1, it is characterised in that: first filter device (7) with
Acidic silicasol product handling system tank (22) connection, the acidic silicasol product handling system tank (22) are equipped with stabilizer feeding inlet
(221).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821675916.7U CN209039069U (en) | 2018-10-16 | 2018-10-16 | Acidic silicasol production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821675916.7U CN209039069U (en) | 2018-10-16 | 2018-10-16 | Acidic silicasol production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209039069U true CN209039069U (en) | 2019-06-28 |
Family
ID=67036152
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821675916.7U Expired - Fee Related CN209039069U (en) | 2018-10-16 | 2018-10-16 | Acidic silicasol production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209039069U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113880095A (en) * | 2020-07-03 | 2022-01-04 | 青岛海湾精细化工有限公司 | Preparation method of acidic silica sol and acidic silica sol |
-
2018
- 2018-10-16 CN CN201821675916.7U patent/CN209039069U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113880095A (en) * | 2020-07-03 | 2022-01-04 | 青岛海湾精细化工有限公司 | Preparation method of acidic silica sol and acidic silica sol |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1330562C (en) | Process of industrialize for waste acid concentrition recovering used in titanium white production by sulfuric acid method | |
| CN106477796A (en) | Desulfurization wastewater treatment system and method | |
| CN105540943A (en) | Silicon-containing wastewater treatment method, silicon-containing wastewater utilization system, molecular sieve preparation method and molecular sieve preparation system | |
| CN107262072A (en) | A kind of industrial production process for carrying zirconium nanocomposite adsorbent | |
| CN105236439B (en) | A kind of bulky grain boric acid and its continuous coo1ing recrystallization preparation technology and device | |
| CN209039069U (en) | Acidic silicasol production system | |
| CN102320630A (en) | Production method of anhydrous sodium sulfate and production equipment thereof | |
| CN101948123B (en) | Technique for manufacturing anhydrous medicinal mirabilite | |
| CN208553163U (en) | A kind of modular horizontal falling film evaporator | |
| CN101209844B (en) | Technique for preparing high quality boric acid from salt lake type boron ore by one-step method | |
| CN206318826U (en) | Desulfurization wastewater treatment system and automatic waste water processing system | |
| CN105152174A (en) | Preparing method for high-purity white carbon black | |
| CN104211072A (en) | Nano silicon dioxide production process technology | |
| CN209039068U (en) | Silica solution production system | |
| CN209193562U (en) | Base exchange method produces silica solution system | |
| CN207079005U (en) | A kind of wire rope factory abraum salt acid treatment device | |
| CN206799175U (en) | A kind of device of thermal phosphoric acid waste heat production liquid sodium silicate | |
| CN215828549U (en) | Intelligent zero-emission system for mine water | |
| CN108246361A (en) | A kind of method for preparing molecular sieve type titanium cerium oxide catalysis material | |
| CN101941721B (en) | Technique for producing medicinal mirabilite by continuous crystallization | |
| CN104548636B (en) | Concentration and evaporation device in zirconium oxychloride production technology | |
| CN208356163U (en) | A kind of energy saving evaporation crystallization equipment of metabisulfite solution | |
| CN208218423U (en) | A kind of sodium carbonate purification and impurity removal system | |
| CN110171840A (en) | A kind of energy-efficient zinc sulfate concentration and crystallization device | |
| CN111533774A (en) | Continuous automatic baicalin extracting and producing process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190628 Termination date: 20211016 |