CN106166401B - Combined type barium sulfate crystallization apparatus - Google Patents
Combined type barium sulfate crystallization apparatus Download PDFInfo
- Publication number
- CN106166401B CN106166401B CN201610672431.1A CN201610672431A CN106166401B CN 106166401 B CN106166401 B CN 106166401B CN 201610672431 A CN201610672431 A CN 201610672431A CN 106166401 B CN106166401 B CN 106166401B
- Authority
- CN
- China
- Prior art keywords
- barium sulfate
- cooling
- crystallisation
- solution
- water pump
- 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
- 238000002425 crystallisation Methods 0.000 title claims abstract description 50
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 title claims abstract description 36
- 230000008025 crystallization Effects 0.000 title claims abstract description 34
- 238000001816 cooling Methods 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims description 3
- 239000000110 cooling liquid Substances 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims description 2
- 238000004781 supercooling Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 15
- 239000013078 crystal Substances 0.000 abstract description 10
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 238000009835 boiling Methods 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 13
- 230000032683 aging Effects 0.000 description 6
- 238000007710 freezing Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- PZZOEXPDTYIBPI-UHFFFAOYSA-N 2-[[2-(4-hydroxyphenyl)ethylamino]methyl]-3,4-dihydro-2H-naphthalen-1-one Chemical compound C1=CC(O)=CC=C1CCNCC1C(=O)C2=CC=CC=C2CC1 PZZOEXPDTYIBPI-UHFFFAOYSA-N 0.000 description 1
- XUBKPYAWPSXPDZ-UHFFFAOYSA-N [Ba].OS(O)(=O)=O Chemical compound [Ba].OS(O)(=O)=O XUBKPYAWPSXPDZ-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/02—Crystallisation from solutions
- B01D9/04—Crystallisation from solutions concentrating solutions by removing frozen solvent therefrom
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0004—Crystallisation cooling by heat exchange
- B01D9/0013—Crystallisation cooling by heat exchange by indirect heat exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0031—Evaporation of components of the mixture to be separated by heating
-
- 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
- C01F11/462—Sulfates of Sr or Ba
Landscapes
- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of combined type barium sulfate crystallization apparatus, barium sulfate solution to be crystallized is positioned over body interior, barium sulfate solution is transported to internal heat exchanger by water pump and exchanged heat with water vapour by servomotor, body interior is again flowed into after heat exchange heating, so constantly circulation, water vapour is flowed into condenser by water vapour pipeline after barium sulfate solution boiling condenses, and incondensible gas is then discharged by non-condensable gas export, solution is cooled down by concentrating feed liquid delivery pipe into crystallisation by cooling tank interior after barium sulfate solution concentration brings up to designated value, crystallization process is then completed in crystallizer, the present apparatus, which takes full advantage of to improve solution concentration and reduce two methods of solution temperature, improves crystallization rate and quality, be advantageous to improve the production efficiency of Barium sulfate crystals.
Description
Technical field
The invention belongs to purification technique field, and in particular to a kind of to heat the combined type knot formed with continuous freezing
Brilliant device.
Background technology
Crystallization process is exactly constantly to form the process that nucleus and nucleus are constantly grown up.The type of crystallizer is a lot, by molten
The method that liquid obtains hypersaturated state can divide crystallizing evaporator and cooler crystallizer；Can decomposition mother solution circulation crystallization device by the type of flow
And magma（That is the mixture of mother liquor and crystal）Circulation crystallization device；It can divide continuous crystalizer and periodic crystallisation device by mode of operation.
Solution degree of supersaturation is the motive force that crystal crystallizes out from solution, and the size of degree of supersaturation directly affects nucleus
Form the speed with rate of crystalline growth.Freezing and crystallizing device is to produce degree of supersaturation, refrigeration crystallization process by reducing temperature
Cryogenic temperature control is extremely important.Traditional freezing and crystallizing device usually uses the single kettle type crystallizer of belt stirrer, and crystallizer is set
Chuck or inner coil pipe cool, and for temperature control near a numerical value, agitating device makes brilliant liquid constantly circulate, low in crystallizer
Caused nucleus is constantly grown up in warm solution, and crystallizer is discharged after reaching the granularity of needs.Also, in continuous crystallization process
In, the speed of growth of crystal is generally unhappy in crystallizer, does not reach desired crystal size, it is necessary to set single aging device,
Crystal is stayed for some time wherein continued growth, aging device is discharged after reaching desired particle diameter.This crystallization apparatus is present
Problems with：
1) in a crystallizer, it is typically only capable to control a crystallization temperature, is not easy effectively control crystallization degree of supersaturation,
So as to can not effectively control the formation of nucleus and the speed of rate of crystalline growth；
2) kettle type crystallization device is cooled by chuck or inner coil pipe, and heat exchange area is small, heat exchange amount is little, is not suitable for big
Rule
Die device；
3) usually cause product grains size uneven because cooling velocity is uneven, the fine grain shadow that crystallization process is formed
Follow-up separation of solid and liquid is rung, or even causes system jams；
4) the usual specification of kettle type crystallization device of belt stirrer is smaller, and disposal ability is limited, large-scale freezing and crystallizing separation
Device is, it is necessary to by the way of the kettle type crystallization device of multiple belt stirrers is in parallel, and number of devices is more, and floor space is big；
5) in continuous crystallization process, the growth residence time of crystal is short in crystallizer, does not reach desired crystal grain
Degree makes brilliant liquid be stayed for some time in aging device, it is necessary to set single aging device, allows crystal continued growth；
6) because aging device is separately provided, make that crystallization apparatus number of devices is more, and floor space is big.Also, low temperature crystallization liquid
The pipeline of aging device is flowed to from crystallizer, in fact it could happen that flow is low, continue crystallization, pipeline turn round situations such as, so as to cause pipeline
Block, influence the continuous operation of device.
7) discharging opening is located at kettle type crystallization device bottom, and the crystal of precipitation easily causes discharging opening blocking after being deposited to bottom.
The content of the invention
The invention provides a kind of combined type barium sulfate crystallization apparatus, can comprehensively utilize heating evaporation and improve solution concentration
Accelerate and improve the advantage of crystallization process and completeness with continuous coo1ing, longtime running is stable, service life length, and operation side
Just safety, technological ability are good.
A kind of combined type barium sulfate crystallization apparatus, servomotor are fixed on ground, and the servomotor is connected with water pump,
And water pump is driven to rotate at a high speed, the input connection main body of water pump, output end then connects heat exchanger, the heat exchanger
Upper end is mounted with feed liquid delivery pipe, and the material flow after supercooling enters in main body, and the upper end of the main body passes through water vapour pipeline
It is connected with condenser, the upper end of condenser installs non-condensable gas export, and lower end is then delivery port.The lower end of aforementioned body and water
Pump is connected, and feed liquid is delivered into crystallisation by cooling tank body by concentrating feed liquid delivery pipe on suitable opportunity and cooled down, institute
State the inside installation crystallisation by cooling component of crystallisation by cooling tank body and be connected with crystallizer.The crystallisation by cooling component includes one-level
Cooling spiral, dividing plate and two level cooling cavities, the one-level cooling spiral are arranged on the upper end of the inside of crystallisation by cooling tank body,
It is filled with cooling water between crystallisation by cooling tank body cavity, and the dividing plate divides one-level cooling spiral and two level cooling cavities
Open.
The pitch of the one-level cooling spiral is equal to its caliber, increases its connecing between cooling liquid as far as possible with this
Contacting surface is accumulated.
The remarkable result of the present invention is：
1st, structure and working principle of the present invention is simple, it is easy to accomplish, personnel's participation depth is low, the crystallization for barium sulfate
Journey, it is easy to implement the automated production of factory.
2nd, the factor of sulfuric acid yield of barium is influenceed in addition to raw mineral materials and the quality of calcining and immersion, is also ceased with crystallization process
Manner of breathing closes, and theoretically the temperature of analysis barium sulfate solution is lower, solution concentration is more big more is advantageous to crystallize, and the present invention is first led to
Cross steam to heat solution, it is reduced the content of moisture after seething with excitement, then cool down acceleration crystallization process again, therefore have more thorough
Bottom and efficient crystallization process.
Brief description of the drawings
Fig. 1 is the general assembly schematic diagram of the present invention, wherein：1- servomotors；2- heat exchangers；3- feed liquid delivery pipes；4- water
Jet chimney；5- non-condensable gas exports；6- condensers；7- delivery ports；8- main bodys；9- concentrates feed liquid delivery pipe；10- crystallisation by cooling
Tank body；11- crystallizers；12- one-level cooling spirals；13- dividing plates；14- two level cooling cavities；15- water pumps.
Fig. 2 is the feed solution flow direction signs of the present invention.
Fig. 3 is the schematic diagram of crystallisation by cooling component of the present invention.
Embodiment
Illustrated below against Fig. 1-3, should before device is operated because plant area's working environment is more severe
The connection of each part of the inspection, the valve set is closed in concentration feed liquid delivery pipe 9, is added into main body 8 to be crystallized
Barium sulfate solution, subsequent start-up servomotor 1, the servomotor 1 drive water pump 15 to move, and observe trial operation situation, so far
Device completes preparation.
When device works, the barium sulfate solution of crystallization is positioned over inside main body 8, and servomotor 1 is by water pump 15 by sulfuric acid
Barium solution is transported to the inside of heat exchanger 2 and exchanged heat with water vapour, is again flowed into after heat exchange heating inside main body 8, so not
Disconnected circulation, water vapour is flowed into condenser 6 by water vapour pipeline 4 after barium sulfate solution boiling condenses, and incondensible
Gas is then discharged by non-condensable gas export 5, and solution is conveyed by concentrating feed liquid after barium sulfate solution concentration brings up to designated value
The one-level cooling spiral 12 that pipe 9 enters inside crystallisation by cooling tank body 10 is cooled down, and subsequently enters two level cooling cavities 14 again
Cooling, crystallization process is finally completed in crystallizer 11, then repeats above-mentioned crystallization process.
Claims (2)
1. a kind of combined type barium sulfate crystallization apparatus, servomotor（1）It is fixed on ground, the servomotor（1）With water pump
（15）Connection, and drive water pump（15）Rotate at a high speed, water pump（15）Input connection main body（8）, its output end then connects
Heat exchanger（2）, the heat exchanger（2）Upper end be mounted with feed liquid delivery pipe（3）, the material flow after supercooling enters main body
（8）In, the main body（8）Upper end pass through water vapour pipeline（4）With condenser（6）Connection, the condenser（6）Install upper end
Non-condensable gas export（5）, lower end is then delivery port（7）, it is characterised in that：Aforementioned body（8）Lower end and water pump（15）Connection,
And on suitable opportunity by feed liquid by concentrating feed liquid delivery pipe（9）It is delivered to crystallisation by cooling tank body（10）Cooled down, institute
State crystallisation by cooling tank body（10）Inside installation crystallisation by cooling component and and crystallizer（11）Connection, the crystallisation by cooling component
Including one-level cooling spiral（12）, dividing plate（13）With two level cooling cavities（14）, the one-level cooling spiral（12）Installed in cold
But tank body is crystallized（10）Inside upper end, in itself and crystallisation by cooling tank body（10）Cavity between be filled with cooling water, it is described
Dividing plate（13）By one-level cooling spiral（12）With two level cooling cavities（14）Separate.
2. combined type barium sulfate crystallization apparatus according to claim 1, it is characterised in that：The one-level cooling spiral（12）
Pitch be equal to its caliber, increase its contact area between cooling liquid as far as possible with this.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610672431.1A CN106166401B (en) | 2016-08-16 | 2016-08-16 | Combined type barium sulfate crystallization apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610672431.1A CN106166401B (en) | 2016-08-16 | 2016-08-16 | Combined type barium sulfate crystallization apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106166401A CN106166401A (en) | 2016-11-30 |
| CN106166401B true CN106166401B (en) | 2018-03-16 |
Family
ID=58065841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610672431.1A Expired - Fee Related CN106166401B (en) | 2016-08-16 | 2016-08-16 | Combined type barium sulfate crystallization apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106166401B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53119782A (en) * | 1977-03-30 | 1978-10-19 | Hitachi Ltd | Crystallizing method for solution containing salt |
| CN202267383U (en) * | 2011-09-29 | 2012-06-06 | 淄博市临淄恒兴化工厂有限公司 | Water immersion type condenser |
| CN203428934U (en) * | 2013-07-24 | 2014-02-12 | 深圳市捷晶能源科技有限公司 | Concentrating and crystallizing system of copper sulfate solution |
| CN104548651A (en) * | 2015-01-19 | 2015-04-29 | 陈式好 | Industrial grade energy-saving and water-saving type MVR (mechanical vapor recompression) continuous evaporative crystallization system |
| CN105797422A (en) * | 2016-04-20 | 2016-07-27 | 西安航天华威化工生物工程有限公司 | Citric acid continuous cooling crystallization system and method thereof |
| CN205965090U (en) * | 2016-08-16 | 2017-02-22 | 广西联壮科技股份有限公司 | Combined type barium sulfate crystallization device |
-
2016
- 2016-08-16 CN CN201610672431.1A patent/CN106166401B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53119782A (en) * | 1977-03-30 | 1978-10-19 | Hitachi Ltd | Crystallizing method for solution containing salt |
| CN202267383U (en) * | 2011-09-29 | 2012-06-06 | 淄博市临淄恒兴化工厂有限公司 | Water immersion type condenser |
| CN203428934U (en) * | 2013-07-24 | 2014-02-12 | 深圳市捷晶能源科技有限公司 | Concentrating and crystallizing system of copper sulfate solution |
| CN104548651A (en) * | 2015-01-19 | 2015-04-29 | 陈式好 | Industrial grade energy-saving and water-saving type MVR (mechanical vapor recompression) continuous evaporative crystallization system |
| CN105797422A (en) * | 2016-04-20 | 2016-07-27 | 西安航天华威化工生物工程有限公司 | Citric acid continuous cooling crystallization system and method thereof |
| CN205965090U (en) * | 2016-08-16 | 2017-02-22 | 广西联壮科技股份有限公司 | Combined type barium sulfate crystallization device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106166401A (en) | 2016-11-30 |
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| Date | Code | Title | Description |
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| C06 | Publication | ||
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| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Su Xuankui Inventor after: Li Chuang Inventor before: Li Qintao Inventor before: Wei Yufen Inventor before: Qin Yi |
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| TA01 | Transfer of patent application right |
Effective date of registration: 20180131 Address after: 530105 standard plant No. 69, No. 12, Chang Gang Avenue, Beijiao Guangxi ASEAN Economic and Technological Development Zone, Nanning City, the Guangxi Zhuang Autonomous Region Applicant after: GUANGXI FANGYUAN MEDICAL TECHNOLOGY CO.,LTD. Address before: 545800, the Guangxi Zhuang Autonomous Region Laibin City Xiangzhou town like stone Applicant before: GUANGXI LIANZHUANG SCIENCE & TECHNOLOGY Co.,Ltd. |
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| TA01 | Transfer of patent application right | ||
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| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: No.12 standard workshop, No.69 Changgang Avenue, Guangxi ASEAN Economic and Technological Development Zone, northern suburb of Nanning City, Guangxi Zhuang Autonomous Region Patentee after: Textile Source Medical Products Group Co.,Ltd. Address before: No.12 standard workshop, No.69 Changgang Avenue, Guangxi ASEAN Economic and Technological Development Zone, northern suburb of Nanning City, Guangxi Zhuang Autonomous Region Patentee before: GUANGXI FANGYUAN MEDICAL TECHNOLOGY Co.,Ltd. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200813 Address after: 530000 first floor, No.2 workshop, No.9 Keyuan West jiulu, high tech Zone, Nanning City, Guangxi Zhuang Autonomous Region Patentee after: Fangyuan group Guangxi Jiahua medical supplies Co.,Ltd. Address before: No.12 standard workshop, No.69 Changgang Avenue, Guangxi ASEAN Economic and Technological Development Zone, northern suburb of Nanning City, Guangxi Zhuang Autonomous Region Patentee before: Textile Source Medical Products Group Co.,Ltd. |
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| 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: 20180316 |