CN205569803U - Industrial mechanical crystallizer of potassium salt - Google Patents
Industrial mechanical crystallizer of potassium salt Download PDFInfo
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- CN205569803U CN205569803U CN201620204469.1U CN201620204469U CN205569803U CN 205569803 U CN205569803 U CN 205569803U CN 201620204469 U CN201620204469 U CN 201620204469U CN 205569803 U CN205569803 U CN 205569803U
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Abstract
Industrial mechanical crystallizer of potassium salt, including crystallizer body, urceolus, draft tube, feed baffle, main agitating unit, calathiform baffle and row's material agitating unit, urceolus, draft tube, feed baffle, calathiform baffle and crystallizer body fixed connection, main agitating unit, row's material agitating unit pass through support and bearing and this body coupling of crystallizer, crystallizer body upper end is equipped with the mother liquor overflow mouth, and the bottom is equipped with the bin outlet, under the calathiform baffle was located the draft tube, the high domes that hang down all around were equipped with the material intercommunicating pore in the middle of the bottom was around the bottom. Utilize the utility model discloses carrying out crystallization production to potassium chloride and potassium sulphide, can making raw materials feed granularity enlarge to 8mm, crystallization circulation ground paste separates with the crystallization product relatively, effectively improves circulation ground paste concentration by mass and crystallizer handling capacity, increase crystallization product granularity, and the raw materials rate of smuggleing secretly in the reduction crystallization product obtains better crystallization effect.
Description
Technical field
This utility model relates to a kind of Potash Industry machinery crystallizer, is specifically related to a kind of slurry circulation that optimizes and flows to and improve the Potash Industry machinery crystallizer crystallizing discharge situation.
Background technology
Machinery crystallization is applied very extensive in the industries such as chemical industry, food, pharmacy, metallurgy, and conventional crystallizer has pressure outer circulation type (FC type) crystallizer, grading type (Oslo type) crystallizer, DTB type crystallizer, DP type crystallizer, Messo type turbulent flow crystallizer.
FC type crystallizer is made up of crystallisation chamber, circulation pipe, circulating pump, heat exchanger etc..Crystallisation chamber has conical bottom, and magma, after the cone end discharges, passes through heat exchanger through circulation pipe axial-flow type circulating pump, after being heated or cooled, enters the most again crystallisation chamber, and so circulation is endlessly.FC type crystallizer is for producing sodium chloride, carbamide, citric acid and some other similar inorganic or organic crystal, and product granularity is between 0.1mm～0.8mm.
Oslo type crystallizer is made up of vaporizer and crystallisation chamber two parts, and the device body of crystallisation chamber has certain taper, and top is big, bottom is little.It is mainly characterized in that the region that degree of supersaturation produces is separately positioned at the two of crystallizer with crystal growth district, crystal is fluidized suspension in circulating mother liquor stream, there is provided a good condition for crystal growth, on the basis of continuous operation, big and uniform crystal can be grown to serve as.The organic salts such as some nitrate and sulfate, sodium chloride, Disodium oxalate., sodium acetate and inorganic salt once produced with this crystallizer.
DTB type crystallizer is the highest crystallizer of a kind of usefulness occurred the fifties in last century, and its crystal property is good, can produce bigger crystal grain, generally up to 0.6mm～1.2mm, production intensity height, and be not easy to scab, and is one of the broad form of continuous crystalizer.The Main Tectonic Characteristics of this type crystallizer is that centre has a guide shell, guide shell surrounding has a cylindrical baffle, in guide shell, lower end is provided with formula agitator arm of boosting, flowed up in guide shell by impeller rotation forces slip during crystallizer work, slip flows downward to crystalliser feet along the annulus between cylinder baffle plate and guide shell again after arriving liquid level, again flow up in being sucked guide shell by impeller again, thus form a closed cycle, crystal is good mixing in cyclic process, again by controlling process regulation solution degree of supersaturation and the crystal growth rate of impact crystallization power, and then make slip constantly grow granularity uniform crystal greatly in this cyclic process.At present, DTB type crystallizer is widely used in chemical industry, food and pharmaceutical industry.
DP type crystallizer is developed in the seventies in last century, it is considered as the improvement of DTB type crystallizer, with DTB type crystallizer differ primarily in that propeller only installed in guide shell by DTB type crystallizer, upwards push circulation fluid, DP type crystallizer is also provided with one group of counter rotating propeller in then annulus outside guide shell, push downwards circulation fluid, inside and outside two groups of propeller synchronous rotaries, promote circulation fluid efficient circulation.The feature of this type crystallizer is that diameter of propeller blade is bigger, wheel speed can be effectively reduced under same loop state, thus reduce secondary nucleation speed, compared with DTB type crystallizer, nucleation rate about declines 1/3, and owing to nucleation amount is greatly reduced, the particle mean size of crystal significantly increases, as a example by ammonium sulfate, crystal size can grow to 0.9mm～1.3mm.But the shortcoming of this type crystallizer is that accuracy of manufacture requirement is high, manufactures, maintenance difficult.
nullMesso type crystallizer is the crystallizer of a kind of newer type，It has two circular concentric mozzles，Outer tube is playpipe、Inner tube is mozzle，The circulation of magma is to be flowed up by mozzle under propeller agitator drives，The most again the annulus in the middle of playpipe with mozzle flows downward，It is similar to DTB type crystallizer，But difference is due to the special tectonic of Messo type crystallizer，The liquid of settling section participates in crystallisation cycle largely，The part of settling section carefully crystalline substance is the most to a certain degree grown to larger particles crystal，Crystallite carefully brilliant content reduces，Crystal size is evenly，As a example by the screen analysis result of potassium chloride product，The potassium chloride of 98.2wt% can grow to 0.42mm～2.36mm,This is that DTB type crystallizer is difficult to accomplish，But this mold structure is complicated，Manufacture and maintaining is the most inconvenient，Some position is scabbed more serious.
Commonly use in potassium salt industry is DTB type crystallizer, such as Chinese patent CN 104722098A, CN 103073030A, but these patents solve the most emphatically crystallization raw material and the crystalline product relative separation problem when crystallization produces, the most do not solve the circulation crystallization problem of bulky grain raw material, more cannot improve the pulp density of race way further, unfavorable to crystal growth, discharge and raising crystallizer treating capacity.Such as CN 103073030A its raw material granularity in actual production controls at below-2mm, discharge concentration 28%～32%, according to its slurry circulation concentration of crystallizer working condition less than 28%, the most unfavorable to grain growth, simultaneously in its underflow discharge system should mainly chloride containing potassium and sodium chloride, but reality still contains the carnallite of 5%～20%；CN 104722098A solves emphatically slip and suffers cutting of sharp guide shell upper and lower side cross section otch in cyclic process, thus cause the problem that crystal grains fine, nucleus increase, it there is also the problem that crystalline product is mingled with certain proportion raw material in actual production, in addition its crystallization raw material is all powder, does not solve crystallization and the circulatory problems of bulky grain raw material.
Utility model content
Technical problem to be solved in the utility model is, overcoming can not be by the deficiency of crystallisation cycle slip Yu crystalline product relative separation in existing potassium salt crystallizer, it is provided that a kind of adaptability to raw material is strong, can increase crystal size, improve crystallizer production efficiency, reduce the Potash Industry machinery crystallizer of underflow crystalline product Central Plains material entrainment rate.
This utility model solves its technical problem the technical scheme is that Potash Industry machinery crystallizer, including crystallizer body, urceolus, guide shell, feed baffle plate, main agitating device, bowl-type baffle plate and discharge agitating device, described urceolus, guide shell, feed baffle plate, bowl-type baffle plate is fixing with crystallizer body to be connected, described main agitating device, discharge agitating device is connected with crystallizer body by support and bearing, described crystallizer body upper end is provided with mother liquor overflow mouth, bottom is provided with discharge gate, described bowl-type baffle plate is positioned at immediately below guide shell, the domes that bottom is low in middle high surrounding, bottom is formed around material intercommunicating pore.
Further, described bowl-type baffle plate hypotenuse and horizontal sextant angle 30 °～45 °, bowl-type baffle plate upper end diameter is more than urceolus lower end diameter, and bowl-type baffle bottom diameter is equal with guide shell lower end diameter, bowl-type baffle bottom central authorities and distance is guide shell lower end diameter 0.7～1.0 times of guide shell lower end.
Further, described material intercommunicating pore is obliquely installed, material intercommunicating pore axis and horizontal sextant angle 15 °～30 °.
Further, described urceolus is horn-like.
Further, described guide shell is horn-like.
Further, described feed baffle plate is cylindrically.
Further, described main agitating device is 4 blade Double helix push type agitating devices or 4 blade single-screw push type agitating devices.
Further, described discharge agitating device is straight 2 blade stirring devices.
This utility model is by arranging bowl-type baffle plate immediately below guide shell, reaction raw materials and crystalline product is made to realize preferable relative separation, crystallizer raw materials for production granularity is not only made to be amplified to 8mm, and the raw material entrainment rate in crystalline product is substantially reduced during bottom discharging, circulation pulp density can be to a certain degree improved during crystallization operation, it is effectively improved crystallizer and produces treating capacity, hence it is evident that improve crystal growth condition, increase crystal growth granularity.
The crystallizer of this utility model band bowl-type baffle plate, both may be used for potassium chloride crystallization and had produced it can also be used to potassium sulfate crystallization produces.Utilize this utility model that potassium chloride and potassium sulfate carry out crystallization to produce, raw material feeding granularity can be made to be amplified to 8mm, crystallisation cycle slip and crystalline product relative separation, it is effectively improved circulation slip mass concentration and crystallizer treating capacity, increase crystalline product granularity, reduce the raw material entrainment rate in crystalline product, it is thus achieved that preferably crystallization effect.
Accompanying drawing explanation
Fig. 1 is the structural representation of this utility model embodiment.
In figure: 1, crystallizer body, 2, mother liquor overflow hole, 3, urceolus, 4, guide shell, 5, feed baffle plate, 6, main agitating device, 7, bowl-type baffle plate, 8, material intercommunicating pore, 9, discharge agitating device, 10, discharge gate；A dissolves district, B crystal region, C mother solution settling section, D crystalline product material discharge region.
Detailed description of the invention
The utility model is described in further detail for lower combination drawings and Examples.
Embodiment
1
With reference to Fig. 1, the present embodiment includes crystallizer body 1, urceolus 3, guide shell 4, feed baffle plate 5, main agitating device 6, bowl-type baffle plate 7 and discharge agitating device 9, described urceolus 3, guide shell 4, feed baffle plate 5, bowl-type baffle plate 7 is connected by welding manner is fixing with crystallizer body 1, described main agitating device 6, discharge agitating device 9 is connected with crystallizer body 1 by support and bearing, described crystallizer body 1 upper end is provided with mother liquor overflow mouth 2, bottom is provided with discharge gate 10, described bowl-type baffle plate 7 is positioned at immediately below guide shell 4, the domes that bottom is low in middle high surrounding, bottom is formed around material intercommunicating pore 8.
In the present embodiment, described bowl-type baffle plate 7 hypotenuse and horizontal sextant angle 32 °, bowl-type baffle plate 7 upper end diameter is more than urceolus 3 lower end diameter, and bowl-type baffle plate 7 base diameter is equal with guide shell 4 lower end diameter, bowl-type baffle plate 7 bottom center and 0.85 times that distance is guide shell 4 lower end diameter of guide shell 4 lower end.
In the present embodiment, described material intercommunicating pore 8 is obliquely installed, material intercommunicating pore axis and horizontal sextant angle 30 °.
In the present embodiment, described crystallizer body 1 upper end drum diameter ￠ 12m, high 5.0m, lower end circular cone hypotenuse and horizontal sextant angle 45 °, high 5.2m.
In the present embodiment, described urceolus 3 in horn-like, upper end drum diameter ￠ 9.6m, high 0.96m, stage casing hypotenuse and horizontal sextant angle 45 °, high 2.4m, lower end cylinder diameter 4.8m, high 1.7m.
In the present embodiment, described guide shell 4 in horn-like, upper end diameter ￠ 4.8m, hypotenuse and horizontal sextant angle 60 °, high 2.1m, lower end cylinder diameter ￠ 2.4m, high 3.0m.
In the present embodiment, described feed baffle plate 5 cylindrically, diameter ￠ 3.6m, high 0.96m.
In the present embodiment, base, described mother liquor overflow hole 2 is away from crystallizer body 1 upper end 0.6m.
In the present embodiment, described bowl-type baffle plate 7 upper end diameter ￠ 6.0m, hypotenuse and horizontal sextant angle 32 °, base diameter 2.4m, high 1.0m, bottom center highest point are away from guide shell lower end 1.7m；Bottoms material intercommunicating pore 6 is evenly arranged, diameter ￠ 0.1m.
In the present embodiment, described main agitating device 6 is 4 blade Double helix push type agitating devices.
In the present embodiment, described crystallizer body 1 bottom discharging mouth diameter 0.3m.
In the present embodiment, described discharge agitating device 9 is straight 2 blade stirring devices.
Using this crystallizer that carnallite carries out cool technology crystallization, raw ore maximum feeding granularity 8mm, race way pulp quality concentration is up to 28%, and crystallizer treating capacity is 70kg/ (h m3), containing carnallite 8% in the crystalline product of underflow discharge, potassium chloride particle mean size 0.32mm, maximum reaches 1.5mm.
Embodiment
2
The present embodiment is with the difference of embodiment 1:
1) crystallizer body upper end drum diameter ￠ 6m, high 2.5m, lower end circular cone hypotenuse and horizontal sextant angle 45 °, high 2.6m；
2) horn-like urceolus upper end drum diameter ￠ 4.8m, high 0.48m, stage casing hypotenuse and horizontal sextant angle 45 °, high 1.2m, lower end cylinder diameter ￠ 2.4m, high 0.8m；
3) horn-like guide shell upper end diameter ￠ 2.4m, hypotenuse and horizontal sextant angle 45 °, high 2.4m, lower end cylinder diameter ￠ 1.2m, high 1.5m；
4) feed cylinder baffle plate diameter ￠ 2.0m, high 0.48m；
5) base, mother liquor overflow hole is away from crystallizer body upper end 0.4m；
6) bowl-type baffle plate upper end diameter ￠ 3.0m, hypotenuse and horizontal sextant angle 45 °, base diameter 1.2m, high 1.5m, bottom center highest point are away from horn-like guide shell lower end 1.0m；Bottoms material intercommunicating pore 4 is evenly arranged, diameter ￠ 0.05m；
7) material intercommunicating pore 8 is obliquely installed, material intercommunicating pore axis and horizontal sextant angle 20 °；
8) main agitating device is 4 blade single-screw push type agitating devices；
9) crystallizer body bottom portion diameter 0.2m.
Using this crystallizer that carnallite carries out cool technology crystallization, raw ore maximum feeding granularity 4mm, crystal region pulp quality concentration is up to 38%, and crystallizer treating capacity is 60kg/ (h m3), containing carnallite 4% in the crystalline product of underflow discharge, potassium chloride particle mean size 0.35mm, maximum reaches 1.5mm.
Embodiment
3
The present embodiment is with the difference of embodiment 1:
1) crystallizer body upper end drum diameter ￠ 6m, high 2.5m, lower end circular cone hypotenuse and horizontal sextant angle 45 °, high 2.6m；
2) horn-like urceolus upper end drum diameter ￠ 4.8m, high 0.48m, stage casing hypotenuse and horizontal sextant angle 45 °, high 1.2m, lower end cylinder diameter ￠ 2.4m, high 0.8m；
3) horn-like guide shell upper end diameter ￠ 2.4m, hypotenuse and horizontal sextant angle 45 °, high 2.4m, lower end cylinder diameter ￠ 1.2m, high 1.5m；
4) it is provided with annular-heating coil pipe outside horn-like guide shell；
5) feed cylinder baffle plate diameter ￠ 2.0m, high 0.48m；
6) base, mother liquor overflow hole is away from crystallizer body upper end 0.4m；
7) bowl-type baffle plate upper end diameter ￠ 4.0m, hypotenuse and horizontal sextant angle 30 °, base diameter 1.2m, high 1.5m, bottom center highest point are away from horn-like guide shell lower end 1.2m；Bottoms material intercommunicating pore 8 is evenly arranged, diameter ￠ 0.1m；
8) material intercommunicating pore 8 is obliquely installed, material intercommunicating pore axis and horizontal sextant angle 15 °.
9) main agitating device is 4 blade single-screw push type agitating devices；
10) crystallizer body bottom portion diameter 0.2m.
Using this crystallizer to carry out the synthetically produced crystallization of potassium sulfate, race way pulp quality concentration is up to 36%, and crystallizer treating capacity is 50kg/ (h m3), sulfur acid potassium 98% in the crystalline product of underflow discharge, potassium sulfate crystal particle mean size 0.30mm, maximum reaches 0.5mm.
Claims (8)
1. a Potash Industry machinery crystallizer, it is characterized in that: include crystallizer body, urceolus, guide shell, feed baffle plate, main agitating device, bowl-type baffle plate and discharge agitating device, described urceolus, guide shell, feed baffle plate, bowl-type baffle plate is fixing with crystallizer body to be connected, described main agitating device, discharge agitating device is connected with crystallizer body by support and bearing, described crystallizer body upper end is provided with mother liquor overflow mouth, bottom is provided with discharge gate, described bowl-type baffle plate is positioned at immediately below guide shell, the domes that bottom is low in middle high surrounding, bottom is formed around material intercommunicating pore.
Potash Industry the most according to claim 1 machinery crystallizer, it is characterized in that: described bowl-type baffle plate hypotenuse and horizontal sextant angle 30 °～45 °, bowl-type baffle plate upper end diameter is more than urceolus lower end diameter, bowl-type baffle bottom diameter is equal with guide shell lower end diameter, bowl-type baffle bottom central authorities and distance is guide shell lower end diameter 0.7～1.0 times of guide shell lower end.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described material intercommunicating pore is obliquely installed, material intercommunicating pore axis and horizontal sextant angle 15 °～30 °.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described urceolus is horn-like.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described guide shell is horn-like.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described feed baffle plate is cylindrically.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described main agitating device is 4 blade Double helix push type agitating devices or 4 blade single-screw push type agitating devices.
Potash Industry the most according to claim 1 and 2 machinery crystallizer, it is characterised in that: described discharge agitating device is straight 2 blade stirring devices.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620204469.1U CN205569803U (en) | 2016-03-17 | 2016-03-17 | Industrial mechanical crystallizer of potassium salt |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620204469.1U CN205569803U (en) | 2016-03-17 | 2016-03-17 | Industrial mechanical crystallizer of potassium salt |
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| CN205569803U true CN205569803U (en) | 2016-09-14 |
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| CN201620204469.1U Withdrawn - After Issue CN205569803U (en) | 2016-03-17 | 2016-03-17 | Industrial mechanical crystallizer of potassium salt |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105597362A (en) * | 2016-03-17 | 2016-05-25 | 化工部长沙设计研究院 | Mechanical crystallizer for sylvite industry |
-
2016
- 2016-03-17 CN CN201620204469.1U patent/CN205569803U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105597362A (en) * | 2016-03-17 | 2016-05-25 | 化工部长沙设计研究院 | Mechanical crystallizer for sylvite industry |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20160914 Effective date of abandoning: 20170825 |
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| AV01 | Patent right actively abandoned |