CN102210941A - Impinging stream evaporation crystallizer - Google Patents
Impinging stream evaporation crystallizer Download PDFInfo
- Publication number
- CN102210941A CN102210941A CN2010101620304A CN201010162030A CN102210941A CN 102210941 A CN102210941 A CN 102210941A CN 2010101620304 A CN2010101620304 A CN 2010101620304A CN 201010162030 A CN201010162030 A CN 201010162030A CN 102210941 A CN102210941 A CN 102210941A
- Authority
- CN
- China
- Prior art keywords
- crystallization
- guide shell
- following
- crystallizer
- guide cylinders
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses an impinging stream evaporation crystallizer. The upper part of a body is provided with a large-diameter evaporation chamber 20; the middle and lower part of the body is provided with a small-diameter crystallization effective volume area, wherein upper and lower guide cylinders 2 are coaxially arranged and upper and lower propellers 3 and 4 in opposite spiral directions are arranged in the two guide cylinders 2; a heat exchange jacket is arranged outside the wall of the crystallization effective volume area; and a vertical heat exchange tube nest 14 is arranged between the inner wall and the upper and lower guide cylinders. The propellers push fluid to flow towards the center of the crystallization effective volume area and impact mutually in the center; the fluid is heated in the process of flowing back through annular chambers between the outer wall and the upper and lower guide cylinders to reach the boiling point, and is boiled and evaporated near the liquid level until reaching an oversaturation state; and the propellers push the oversaturated suspensoid to flow towards the center for impact again, recycle is formed, and the crystallization process is completed through impact and the subsequent circular flow. The impinging stream evaporation crystallizer is applied to the parallel evaporation-crystallization process, simplifies flows and equipment, has the outstanding advantages of high efficiency and energy conservation, and reduces the probability of scarring of crystals on the heating surface.
Description
Affiliated technical field:
Belong to physics, chemical process equipment.Be applicable to solution walk abreast evaporative crystallization, produce the process of crystalline product or intermediate products.
Background technology:
In industries such as chemical industry, medicine, light industry, there are many solid products to make by crystallization from solution.Crystallization is carried out under the oversaturated condition of solution from solution.According to producing supersaturation mode difference, crystallization process is broadly divided into three types of crystallisation by cooling, evaporative crystallization and reactive crystallizations; Wherein crystallisation by cooling is most widely used.
Crystallisation by cooling normally carries out the crystallisation by cooling operation to the solution evaporation and concentration to certain near changing crystallization apparatus over to after the saturated concentration.The cooler crystallizer of commercial Application has a variety of.The crystallizer of one class band guide shell of research and development 1950 to the seventies, DTB crystallizer (Mullin.J.W. for example, " Industrial Crystallization " pp1-168, Plenum Press, New York, 1976), DP crystallizer (west of a river daf, " a month island formula DP type crystalline substance goes out device ", other volume chemical industry, 18 (2): 58-65,1974) and Standard-Messo turbulent flow crystallizer (Messing, T., Br.Chem.Eng., 14:641-645,1969) etc., still belong to more advanced continuous crystallisation device so far.The main weak point of above-mentioned crystallizer is that the microcosmic troubled water is undesirable, and the relatively poor material of some crystallographic property still is difficult to make thick uniform crystallization.Wu Yuan etc. newly research and develop on project of national nature science fund project research basis and " irrotationality percussion flow vacuum crystallizer " (patent No. ZL 2,007 2 0083842.3) of patenting and " irrotationality percussion flow heat exchange type crystallizer " (ZL200820066743.9) utilize the liquid continuous phase percussion flow effectively to promote the characteristic that microcosmic mixes, degree of supersaturation environment very uniformly can be provided, significantly improve the condition of nucleus generation and crystalline growth, be better than above various crystallization apparatus; Though their implement the mode difference of cooling, promptly respectively with the mode cooling working medium of vacuum and heat exchange.
For the production of some product, will evaporate or part evaporation process and crystallization process be combined in carry out in the same equipment more reasonable, can simplify flow process, aspect such as energy-conservation produces significant benefit.Yet not seeing as yet so far has the high performance technology equipment that is specifically designed to parallel evaporate-crystallization process.
For overcoming above-mentioned the deficiencies in the prior art, research and development the present invention.
Summary of the invention:
Purpose of the present invention provides that a kind of microcosmic mixes, power consumption is low, can save energy the technical equipment of finishing parallel evaporate-crystallization process efficiently.
Percussion flow crystallizing evaporator of the present invention, by a middle and lower part is crystal region than minor diameter, top is for than major diameter band top cover 6 and be furnished with the vaporization chamber 20 of steam outlet pipe 9, bottom centre is furnished with the pot shape or the upright cylinder 1 of conical bottom reducing of the classification leg 11 of band circulating mother liquor inlet tube 12 and magma outlet 13, vertical coaxial be installed in cylinder 1 crystal region on, following two inwalls are equipped with the guide shell 2 of some vertical baffling baffle plates 5, coaxially be installed in respectively, the hand of spiral is opposite in following two guide shells 2, pass through last from the upper and lower propelling fluid respectively, following guide shell 2 is on crystal region center flow bump, following two screws 3 and 4, be arranged on the upright cylinder 1 middle and lower part inwall and last of reducing, vertical heat exchanging pipe 14 between the following guide shell 2, the heat exchange jacket 17 that the upright cylinder 1 middle and lower part wall of reducing is outer, with and outlet be arranged on, feed pipe 7 between the following guide shell 2 is formed.The outlet of feed pipe 7 also can be arranged in or descend the import department of guide shell 2.
Be different from and existingly be used to evaporate or the technical equipment of crystallization process, the present invention's " percussion flow crystallizing evaporator " can be directly used in parallel evaporate-crystallization process, simplify flow process, aspect such as energy-conservation produces significant benefit.Have following advantage in addition: (1) utilizes the percussion flow microcosmic to mix very effective characteristic promotion crystallization process; (2) power is significantly saved in the fluidal texture arrangement of vertical coaxial two stream percussion flows; (3) arrangement of vertical heat exchanging pipe has reduced the probability that crystallization scabs on the heat exchange wall.
Description of drawings:
Fig. 1 is a percussion flow crystallizing evaporator structural representation of the present invention, and it has represented its working principles simultaneously; Fig. 2 is the A-A cross sectional plan view of Fig. 1.
The basic element of character of the technology of the present invention equipment comprises the upright cylinder 1 of reducing, and its top is for than major diameter band arch or back taper top cover 6 and be furnished with the vaporization chamber 20 of steam outlet pipe 9, and the middle and lower part be the crystal region than minor diameter, and the bottom is pot shape or taper.Upper and lower two guide shells 2 of vertical coaxial installation and be installed in last screw 3 and following screw 4 in two guide shells 2 coaxially respectively in the middle and lower part crystal region of cylinder 1.Two screws 3 are opposite with 4 hands of spiral, a dextrorotation, another is left-handed, and respectively propelling fluid flows downwards and upwards and place's bump in opposite directions in the middle of upper and lower guide shell 2, constitute vertical coaxial two stream percussion flows, and between upper and lower guide shell 2, form impingement region IZ.The space that reducing cylinder 1 middle and lower part smaller diameter portion and conical bottom thereof are surrounded is the dischargeable capacity district of crystallization process, it also is the solution thermal treatment zone, wherein adorning processing medium is crystallization-solution mixture suspended substance, and liquid level guide shell 2 certain altitudes of not going up, and guarantees to realize stable percussion flow fluidal texture.Upper and lower two guide shell 2 inwalls are respectively adorned the some vertical baffling baffle plates 5 that are uniformly distributed along the circumference, and rotate the rotational flow that causes to suppress screw.The upright cylinder 1 middle and lower part wall of reducing is outward a crystal region peripheral hardware displacement thermal jacket 17; Between this part inwall and the upper and lower guide shell 2 vertical heat exchanging pipe 14 is set, the two feeds steam or other heat medium with the flow through processing medium of their walls of indirect, is furnished with heat medium inlet tube 18,15 and outlet 19,16 respectively.Connect under the conical bottom of cylinder 1 and eluriate leg 11, its bottom connects circulating mother liquor entrance sleeve 12, and lower sides is furnished with the discharge duct 13 that magma is finished product crystallization and mother liquor mixture S.It is in the impingement region IZ that the outlet of material liquid feed pipe 7 is arranged between the upper and lower guide shell 2; This outlet also can be arranged in or following guide shell 2 entrance points.Last screw 3 passes top cover 6 centers with the common drive shaft of following screw 4 and is connected motor.
The specific embodiment:
Technical equipment of the present invention generally adopts the continued operation mode.
During operation, the processing medium of packing into earlier in the crystallization dischargeable capacity district, reducing cylinder 1 middle and lower part is crystallization and mother liquor mixture suspended substance, the feeding liquid of also can packing into; Start screw 3 and 4 then; Simultaneously constantly send into steam V or other heat medium to heat exchanging pipe 14 and chuck 17 respectively by entrance sleeve 15 and 18; Condensed water L flows out by outlet 16 and 19 after the heat exchange.Wait to flow and temperature all reach stable after, begin to add feedstock solution F continuously and stably by feed pipe 7.Screw 3 and 4 propelling fluids (processing medium) flow to middle part, crystallization dischargeable capacity district from the upper and lower through guide shell 2 respectively, and clash in opposite directions at this place, form impingement region IZ around striking face.Between fluid from different directions in this district violent relative motion make between stream group with liquid-solid phase between mix effectively and contact, states such as temperature, liquid concentration almost reach the molecule uniformity coefficient.Behind the bump, the ring casing about the suspended substance process between guide shell 2 outer walls and the cylinder 1 middle and lower part inwall returns the upper/lower terminal in crystallization dischargeable capacity district respectively.In flow through vertical heat exchanger tube 14 and heat exchange jacket 17 wall processes,, reach the boiling point at liquid level place, crystallization dischargeable capacity district by the steam in heat exchanger tube and the chuck or other heat transferring medium indirect.Return near solution explosive evaporation liquid level of upper end, crystallization dischargeable capacity district, the indirect steam of generation is discharged by steam outlet pipe 9.Vaporization chamber 20 adopts than major diameter with control steam flow rate upwards, thereby can rely on gravity settling separation to fall the drop or the liquid foam of most of entrainment with steam.According to the specific requirement that whether utilizes indirect steam and utilization, the vapor-liquid separating device that adds can also be arranged in the downstream of steam outlet pipe 9.
Crystallization-solution suspension that evaporation back solution concentration increases, reaches hypersaturated state is flowed to middle part, crystallization dischargeable capacity district by last screw 3 conveyings by last guide shell 2 again, with return lower end, crystallization dischargeable capacity district, carried the suspended substance that flows to this place to clash into once more by following screw 4 by guide shell 2 down again, circulation so repeatedly.Crystallization comprises that nucleus generates and crystal growth, circulates in the process after being clashed into repeatedly and clashed into by upper and lower screw 3 and 4 promotion suspended substances and finishes.
Circulate in the process some crystallization-solution suspension and enter classification leg (also claiming to eluriate leg) 11.Infusion pump a with suitable kind extracts a certain amount of circulating mother liquor from the cofferdam 8 that is arranged on crystallization dischargeable capacity district upper portion side wall, send into elutriation leg 11 by the circulating mother liquor entrance sleeve 12 of circulating line b and elutriation leg 11 bottoms and also upwards flow, the crystalline particle in the elutriation leg is carried out hydraulic classiciation.The crystalline particle of having grown up and the suspended mixture of partial mother liquid move downward, and are magma S, and the discharge duct 13 through eluriating leg lower sides place draws off, and separator such as the centrifuge of delivering to suitable kind separate or/and obtain crystalline product after the drying; The crystalline particle of not growing up is as yet carried by circulating mother liquor and moves upward, and returns the dischargeable capacity district continued growth of crystallizer through elutriation leg 11.Infusion pump a among Fig. 1 and the pipeline b that is represented by dotted lines are matching used elements, do not belong to percussion flow crystallizing evaporator of the present invention itself.
The outstanding advantage of percussion flow crystallizing evaporator of the present invention is to be used for parallel evaporate-crystallization process effectively, has remedied the deficiencies in the prior art; To the production process of many crystalline products, can simplify technological process and equipment greatly.In addition, it also has following advantage: the characteristics that (1) utilizes percussion flow to strengthen the microcosmic mixing can be crystallization process provides uniform degree of supersaturation environment, promotes that crystallization process carries out effectively; (2) special mobile structure arrangement makes it to have the considerable energy saving characteristic; (3) adopt vertical heat exchanging pipe up and down between guide shell 2 and reducing cylinder 1 middle and lower part inwall, reduced the probability that crystallization scabs on the heat exchange wall.
Claims (2)
1. a crystallizer is evaporated in percussion flow, it is characterized in that it is the crystal region than minor diameter by a middle and lower part, top is for than major diameter band top cover 6 and be furnished with the vaporization chamber 20 of steam outlet pipe 9, bottom centre is furnished with the pot shape or the upright cylinder 1 of conical bottom reducing of the classification leg 11 of band circulating mother liquor inlet tube 12 and magma outlet 13, vertical coaxial be installed in cylinder 1 crystal region on, following two inwalls are equipped with the guide shell 2 of some vertical baffling baffle plates 5, coaxially be installed in respectively, the hand of spiral is opposite in following two guide shells 2, pass through last from the upper and lower propelling fluid respectively, following guide shell 2 is on crystal region center flow bump, following two screws 3 and 4, be arranged on the upright cylinder 1 middle and lower part inwall and last of reducing, vertical heat exchanging pipe 14 between the following guide shell 2, the heat exchange jacket 17 that the upright cylinder 1 middle and lower part wall of reducing is outer, with and outlet be arranged on, feed pipe 7 between the following guide shell 2 is formed.
2. evaporate a crystallizer by the described percussion flow of claim 1, the outlet that it is characterized in that feed pipe 7 also can be arranged in or the import department of guide shell 2 down.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101620304A CN102210941A (en) | 2010-04-08 | 2010-04-08 | Impinging stream evaporation crystallizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101620304A CN102210941A (en) | 2010-04-08 | 2010-04-08 | Impinging stream evaporation crystallizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102210941A true CN102210941A (en) | 2011-10-12 |
Family
ID=44742618
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010101620304A Pending CN102210941A (en) | 2010-04-08 | 2010-04-08 | Impinging stream evaporation crystallizer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102210941A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105194900A (en) * | 2015-07-22 | 2015-12-30 | 成都百味坊贸易有限公司 | Alga iodate evaporating crystallizer |
| CN106390506A (en) * | 2016-10-18 | 2017-02-15 | 阿坝州高远锂电材料有限公司 | Continuous crystallizer |
| CN106422400A (en) * | 2016-10-18 | 2017-02-22 | 阿坝州高远锂电材料有限公司 | Crystallizer |
| CN106582056A (en) * | 2016-12-26 | 2017-04-26 | 江苏乐科节能科技股份有限公司 | Double-stroke forced circulation type heat exchange and crystallization integrated device and working method thereof |
| CN107961557A (en) * | 2017-10-24 | 2018-04-27 | 湖北民族学院 | The apparatus and method of rapid crystallization of biomolecules |
| CN108635900A (en) * | 2018-05-26 | 2018-10-12 | 江苏源拓环境科技有限公司 | A kind of compact micro-pressure-difference push in circulating and evaporating concentration and crystallization apparatus |
| CN112221169A (en) * | 2019-07-15 | 2021-01-15 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization system |
| CN114956230A (en) * | 2022-05-30 | 2022-08-30 | 沈阳工业大学 | Cavitation impinging stream evaporator |
-
2010
- 2010-04-08 CN CN2010101620304A patent/CN102210941A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105194900A (en) * | 2015-07-22 | 2015-12-30 | 成都百味坊贸易有限公司 | Alga iodate evaporating crystallizer |
| CN106390506A (en) * | 2016-10-18 | 2017-02-15 | 阿坝州高远锂电材料有限公司 | Continuous crystallizer |
| CN106422400A (en) * | 2016-10-18 | 2017-02-22 | 阿坝州高远锂电材料有限公司 | Crystallizer |
| CN106422400B (en) * | 2016-10-18 | 2018-08-28 | 阿坝州高远锂电材料有限公司 | A kind of crystallizer |
| CN106582056A (en) * | 2016-12-26 | 2017-04-26 | 江苏乐科节能科技股份有限公司 | Double-stroke forced circulation type heat exchange and crystallization integrated device and working method thereof |
| CN107961557A (en) * | 2017-10-24 | 2018-04-27 | 湖北民族学院 | The apparatus and method of rapid crystallization of biomolecules |
| CN107961557B (en) * | 2017-10-24 | 2020-03-17 | 湖北民族大学 | Apparatus and method for rapid crystallization of biomolecules |
| CN108635900A (en) * | 2018-05-26 | 2018-10-12 | 江苏源拓环境科技有限公司 | A kind of compact micro-pressure-difference push in circulating and evaporating concentration and crystallization apparatus |
| CN112221169A (en) * | 2019-07-15 | 2021-01-15 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization system |
| CN114956230A (en) * | 2022-05-30 | 2022-08-30 | 沈阳工业大学 | Cavitation impinging stream evaporator |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102210941A (en) | Impinging stream evaporation crystallizer | |
| CN206518915U (en) | Force interior circulation crystallizer | |
| CN104162288B (en) | A kind of spiral-flow type fluidized-bed crystallizer | |
| CN103071310B (en) | Evaporating crystallizer | |
| CN103159194B (en) | Continuous crystallization process for monopotassium phosphate | |
| CN108939599A (en) | A kind of self-loopa crystallizer and multistage continuous crystallisation process | |
| CN101531382B (en) | Production process and crystallization device for large-particle ammonium sulfate | |
| CN109173324A (en) | A kind of potassium nitrate continuous crystallisation device and method | |
| CN104984557A (en) | Five-effect eight-body crystallization and evaporation process | |
| CN109011682A (en) | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator and method | |
| CN108714311A (en) | A kind of vertical vacuum crystallization apparatus | |
| CN209089953U (en) | Cooling tank is used in liquid quelite production | |
| CN215310307U (en) | Cooling crystallization device | |
| CN208525882U (en) | Vacuum flash evaporation mould and multistage flash distillation crystallization apparatus | |
| CN201692685U (en) | Impinging stream evaporating crystallizer | |
| CN203816265U (en) | Inorganic salt continuous crystallization device | |
| CN201182916Y (en) | Irrotational impact-flow heat exchange type crystallizer | |
| CN203196371U (en) | Continuous potassium dihydrogen phosphate crystallization device | |
| CN205340185U (en) | Continuous crystallization equipment of multistage high vacuum insulation flash distillation | |
| CN209138035U (en) | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator | |
| CN104740891B (en) | Air cooling crystallizer for inner fin tubes | |
| CN107626112A (en) | A kind of continuous production vacuum cooling crystallizer | |
| CN208990815U (en) | A kind of cage stirring crystallizing evaporator | |
| CN204034311U (en) | A kind of spiral-flow type fluidized-bed crystallizer | |
| CN213221025U (en) | Control system for improving potassium chloride particle size in potassium-sodium separation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| DD01 | Delivery of document by public notice |
Addressee: Wu Yuan Document name: Notification of Publication of the Application for Invention |
|
| DD01 | Delivery of document by public notice |
Addressee: Wu Yuan Document name: Notification of before Expiration of Request of Examination as to Substance |
|
| DD01 | Delivery of document by public notice |
Addressee: Wu Yuan Document name: Notification that Application Deemed to be Withdrawn |
|
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20111012 |