CN208711101U - A kind of vertical vacuum crystallization apparatus - Google Patents

Abstract

The utility model provides a kind of vertical vacuum crystallization apparatus, including crystallization unit and condensation part, crystallization unit is located at below condensation part, and crystallization unit includes crystallized region cylinder, external flow guiding cylinder, central draft tube, bottom blender, secondary steam rising cylinder, circulating pump, inner cycle channel and outside the circular channels；Condensation part includes condensation segment cylinder and overflow weir, the first water stopping cap, folding pendular ring and the second water stopping cap that condensation segment inner barrel is from top to bottom set gradually；The utility model has the advantages that: it is not required to heat exchanger, there is no inner surface serious scales and fouling to clear up problem；Vacuumizing pressure is close with solution vapor partial pressure, operates more stable.Crystallization unit and condensation part are combined into an equipment, shorten secondary steam flow path, eliminate the increased seal point leakage because of pipeline connection.Inner cycle channel eliminates high saturation region in crystallization unit, and saturation degree is relatively uniform and lower everywhere, and outside the circular channels eliminate excessive fine grain, while eluriating out the product of Unusually narrow particle size distribution.

Description

A kind of vertical vacuum crystallization apparatus

Technical field

The utility model relates to chemical separating fields, and in particular to a kind of vertical vacuum crystallization apparatus.

Background technique

Crystallization refers to the process of that solid is precipitated from gas, liquid or fusant with crystal state, this process is by heating power It learns and kinetic factor determines, solute will be precipitated from solution, it is necessary to constantly obtain energy from outside, make in solution solution not Disconnected evaporation reaches saturation and supersaturation, (is in stable region) when solution is not up to saturated, and solute will not generate crystallization, when When solution is between solubility curve and supersolubility curve (Metastable zone), lolute crystallization and dissolution are flat in dynamic at this time Weighing apparatus, solute will not spontaneous nucleation be precipitated, if having nucleus enter can grow crystal, this stage is easily influenced by the external world, i.e., whether there is or not Crystal seed, crystal seed size, it is how many, have the factors such as without mixing, vibration and impurity, the growth of crystal should control to be carried out in this area. It, then can the spontaneous more nucleus of generation after solution enters supersaturated area (range of instability).The formation of nucleus is divided into two classes, and no crystal is deposited Primary nucleation and have a secondary nucleation existing for crystal, during industrial crystallization, usually control secondary nucleation, i.e. fluid Shear stress nucleation and Crystallisation, that is, select suitable stirring pattern and revolving speed.

According to the universal diffusion theory analysis of chemical engineering unit operation, the growth of crystal is related with following factor:

(1) motive force of crystal growth is the supersaturation concentration difference and transmission speed of solution, the solute in supersaturated solution The opposing stationary liquid layer being diffused near nucleus, and pass through opposing stationary solution layer and reach plane of crystal insertion crystal face, make its crystalline substance Body is grown up, and releases crystallization heat, and heat is transmitted in solution by diffusion again.

(2) temperature of solution, at the same time and under the conditions of identical supersaturation concentration difference, temperature is higher, and solution is viscous Degree is lower, and the diffusion velocity of solution is faster, and the growth rate of crystal is also fast, is more easy to get the biggish crystal of partial size.

(3) circulation solution flow, when one timing of evaporation capacity is same, the flow of circulation solution and the degree of supersaturation of solution are inversely proportional Functional relation, and circular flow has determined the flow velocity size at each position of crystallizing evaporator, flow velocity great Yi cause between crystal, are brilliant Aggravation is collided between body and wall, is caused crystal fracture at increase a possibility that secondary nucleus, product cut size is influenced also very big； Flow velocity is small, is unfavorable for the growth of crystal, therefore to have circular flow appropriate.

(4) magma concentration, under the premise of other conditions are certain, magma concentration height then crystal ownership in crystallizing evaporator More, the crystal residence time increases, and is conducive to the elimination and crystal growth of solution degree of supersaturation, but magma excessive concentration, crystal it Between, collision probability increases between crystal and wall, the probability that crystal is fractured into secondary nucleus is also more, also not to crystal growth Benefit, so crystal concentration appropriate should be controlled, general solid-to-liquid ratio control is 20%.

(5) fine crystal elimination, grain is too many in magma, has excessively digested solution degree of supersaturation, has influenced other crystal Growth, is also unfavorable for the separation of subsequent handling, and commercial use is too small, needs to inject the brilliant water that disappears, dissolves fine crystals, with control Grain number density is generated compared with coarse crystal product.

It is at present using pressure outer circulation using more method for crystallising, feed liquid self-loopa pipe lower part is added, and ties with leaving After the magma mixing of brilliant room bottom, from pumping toward heating room.Magma is heating indoor heating (usually 2 ~ 6 DEG C), but does not occur Evaporation.Hot magma boils after entering crystallisation chamber, and solution is made to reach hypersaturated state, and then part deposition of solute is in suspension crystal grain table On face, crystal is made to grow up.Magma as product is discharged from circulation pipe top.Forced-circulation evaporation production capacity of crystallizer for co-production of ammonium is big, But since device without mixing inside the crystallizer leads to the broad particle distribution of product so that the degree of mixing of slurry is deteriorated；And It is cooling since there are outer circulations in the equipment, so its cooling tube can be easier fouling.

Utility model content

A kind of in order to solve the above problems, the utility model proposes vertical vacuum crystallization apparatus.

The technical solution of the utility model is: a kind of vertical vacuum crystallization apparatus, characterized by comprising: crystallization unit and Condensation part；

The crystallization unit include crystallized region cylinder, external flow guiding cylinder, central draft tube, bottom blender, secondary steam rise cylinder, Circulating pump, inner cycle channel and outside the circular channels；

The crystallized region cylinder is the axially symmetric structure with central axis, including be sequentially connected taper type top, straight tube In the middle part of shape and conical lower portion, the straight tube shape middle part includes top and bottom, the big circular bottom surface on the taper type top and institute It states upper end to be connected, the bottom surface of the conical lower portion is connected with the lower end, and the middle position in the middle part of the straight tube shape offers clear Clear solution outlet symmetrically offers feeding inlet and discharge port using the central axis as symmetry axis in the conical lower portion；

The external flow guiding cylinder includes opposite first end and second end, and the external flow guiding cylinder is located at the crystallized region cylinder Inside, and the first end is handed in the middle part of the variable diameter and the straight tube shape by being fixedly connected in the middle part of variable diameter and the straight tube shape The top that place is located at the clear solution outlet is connect, the lower end in the middle part of the second end and the straight tube shape is in same horizontal line On, the external flow guiding cylinder is with the central axis axial symmetry；

The central draft tube includes opposite third end and the 4th end, and the central draft tube is located at the external flow guiding cylinder Inside, and the horizontal plane where the third end is higher than the position that the external flow guiding cylinder intersects with straight tube shape middle part, institute The liquid level for stating third end top is evaporation interface, and the 4th end is lower than the second end in horizontal plane in the height of horizontal plane Highly, the central draft tube is with the central axis axial symmetry；

The bottom blender is located at the inside at the 4th end；

The secondary steam rises cylinder and is cylindrical structure and is connected with the top on the taper type top and in described Mandrel axial symmetry；

The circulating pump is located at the outside of the crystallized region cylinder, and molten by pipeline and the feeding inlet and the clarification Liquid outlet is connected；

Channel in the cylinder of the central draft tube and between the external flow guiding cylinder and the central draft tube forms institute State inner cycle channel；

Channel between the external flow guiding cylinder and the cylindrical central part is settling section, the inner cycle channel, described clear Clear area, the circulating pump and the pipeline form the outside the circular channels；

The condensation part includes condensation segment cylinder and the overflow that the condensation segment inner barrel is from top to bottom set gradually Weir, the first water stopping cap, folding pendular ring and the second water stopping cap, the condensation segment cylinder, the overflow weir, first water stopping cap, institute Folding pendular ring and second water stopping cap are stated with the central axis axial symmetry, the condensation part is located at the upper of the crystallization unit Side, and the condensation segment cylinder bottom cap residence states secondary steam and rises the outside that cylinder is fixedly connected on the taper type top, The lower edge of the overflow weir and the condensation segment cylinder are tightly connected, and the top of the overflow weir is diametrically less than or equal to described The water blocking width of first water stopping cap, the folding pendular ring are and described between first water stopping cap and second water stopping cap The outer edge of folding pendular ring is fixed on the condensation segment cylinder, and the internal diameter of the folding pendular ring is less than or equal to first water stopping cap Water blocking width, and it is less than or equal to the water blocking width of second water stopping cap, the condensation segment cylinder is set in the overflow weir position There is coolant liquid inlet.

Preferably, the bottom blender is propeller agitator, to push away the mixed solution in the central draft tube The evaporation interface for entering the central draft tube top improves the interior cycle efficieny in inner cycle channel.

Preferably, the top of the condensation segment cylinder offers on-condensible gas outlet, on-condensible gas outlet position In the top of the overflow weir, the condensation segment cylinder is discharged in the fixed gas in secondary steam.

Preferably, it is connected to the fine grain waterpipe that disappears on the pipeline on the outside of the clear solution outlet, to the fine grain water that will disappear It is mixed with crystallization solution, eliminates the fine grain in crystallization solution.

Preferably, condensation segment cylinder lower part offers cooling condensation mixed liquor outlet, the cooling condensation mixing The height off the ground of liquid outlet is less than the height off the ground that the secondary steam rises cylinder steam output end.

Preferably, the condensation part further includes liquid seal trough and barometric pipe, and one end of the barometric pipe and the cooling condense Mixed liquor outlet is connected, and the other end of the barometric pipe accesses the liquid seal trough, to the condensation segment cylinder is intracorporal cold But condensation mixed liquor successfully lead in the liquid seal trough, in the barometric pipe in the hydraulically full and described barometric pipe fluid column away from Ground height is between 10 ~ 20 meters, to make cooling condensation mixed liquor by fluid column gravity automatically into the liquid seal trough.

Preferably, the fluid-tight trench bottom offers coolant liquid and removes heating gate, and the coolant liquid goes heating gate to pass through circulation Pipeline is connected with the coolant liquid inlet.

Preferably, the barrel dliameter of the external flow guiding cylinder is twice of the central draft tube barrel dliameter, to give the outer circulation Channel provides adequate space, to eliminate excessive fine grain and eluriate the granularity of product.

Preferably, the crystallization unit further includes product shurry pump, and the product shurry pump passes through pipeline and the discharge port It is connected, the crystallization to generate the crystallization unit is drawn.

Preferably, the vertical vacuum crystallization apparatus is plural serial stage framework, two neighboring vertical vacuum crystallization apparatus The outlet end of one of them circulating pump wherein another feeding inlet phase with two neighboring vertical vacuum crystallization apparatus simultaneously Even.

Compared with prior art, a kind of vertical vacuum crystallization apparatus main equipment of the utility model is simple, is not required to exchange heat Device, there is no inner surface serious scales and fouling to clear up problem, to influence production capacity；Vacuumizing pressure and solution steam Vapour partial pressure is close, operates more stable.Crystallization unit and condensation part are combined into an equipment, are different from the crystallization and evaporation of other forms Device and condenser be it is separated, major advantage is: do not need with pipeline by secondary steam from crystallization unit introduce condensation part, shorten Secondary steam flow path is eliminated because the resistance of ducting causes secondary steam to overheat, and increases cooling liquid measure；It eliminates because pipeline connects And increased seal point leakage, and increase the sucking rate of vacuum system；The evaporation that solution balances each other with vacuum is also reduced simultaneously Temperature improves the evaporation capacity of solution, has saved power energy consumption, while having saved equipment investment.The interior circulation of the utility model High saturation region in crystallizer is eliminated in channel, and saturation degree is relatively uniform and lower everywhere in crystallizer, and it is strong to improve evaporation Degree, enhances the production capacity of crystallizer, propeller agitator application improves interior cycle efficieny, reduces crystal and blade Broken nucleation probability is collided, blender uses frequency control, is more conducive to adjustment produce load；Outside the circular channels eliminate excess Fine grain and product granularity elutriation, guarantee produce Unusually narrow particle size distribution product.

Detailed description of the invention

Fig. 1 is a kind of overall structure diagram of vertical vacuum crystallization apparatus of the utility model.

Specific embodiment

To make to have further understanding to the purpose of this utility model, construction, feature and its function, hereby cooperate embodiment Detailed description are as follows.

Referring to Fig. 1, Fig. 1 is a kind of vertical vacuum crystallization apparatus overall structure diagram of the utility model, such as Fig. 1 institute Show, the vertical vacuum crystallization apparatus of an embodiment of the present invention, including crystallization unit 1 and condensation part 2.

Crystallization unit 1 includes crystallized region cylinder 3, external flow guiding cylinder 4, central draft tube 5, bottom blender 6, secondary steam rising cylinder 7, circulating pump 8, inner cycle channel and outside the circular channels.

Crystallized region cylinder 3 is the axially symmetric structure with central axis 31, including be sequentially connected taper type top 32, straight tube Shape middle part 33 and conical lower portion 34, straight tube shape middle part 33 includes upper end 331 and lower end 332, the big round bottom on taper type top 32 Face is connected with upper end 331, and the bottom surface of conical lower portion 34 is connected with lower end 332, and 33 middle position offers clear in the middle part of straight tube shape Clear solution outlet 35 with central axis 31 is symmetry axis in conical lower portion 34, symmetrically offers feeding inlet 36 and discharge port 37. Taper type top 32 is concentrated for secondary steam, and conical lower portion 34 is more advantageous to the magma that the crystallization generated in crystallization unit 1 is formed It concentrates, convenient for drawing.

External flow guiding cylinder 4 includes opposite first end 41 and second end 42, and external flow guiding cylinder 4 is located at the inside of crystallized region cylinder 3, And first end 41 is fixedly connected by variable diameter 43 in the middle part of straight tube shape 33,33 junctions are located at clarification in the middle part of variable diameter 43 and straight tube shape In the same horizontal line, external flow guiding cylinder 4 is with 31 axial symmetry of central axis for the top of solution outlet 35, second end 42 and lower end 332.

Central draft tube 5 includes opposite third end 51 and the 4th end 52, and central draft tube 5 is located at the interior of external flow guiding cylinder 4 Portion, and the horizontal plane where third end 51 is higher than external flow guiding cylinder 4 and 33 positions intersected in the middle part of straight tube shape, 51 top of third end Liquid level is evaporation interface 19, and the 4th end 52 is lower than height of the second end 42 in horizontal plane, central draft tube 5 in the height of horizontal plane With 31 axial symmetry of central axis.Bottom blender 6 is located at the inside at the 4th end 52.

Secondary steam rises cylinder 7 and is cylindrical structure and is connected with the top on taper type top 32 and with 31 axis pair of central axis Claim.

Circulating pump 8 is located at the outside of crystallized region cylinder 3, and passes through pipeline 9 and feeding inlet 36 and clear solution outlet 35 It is connected.

Channel in the cylinder of central draft tube 5 and between external flow guiding cylinder 4 and central draft tube 5 forms inner cycle channel. Interior cycle efficieny is high, magma density can be made to be maintained at 30~40% levels, and can eliminate high saturation region, each in crystallizer It is relatively uniform and lower to locate saturation degree, thus enhances the production capacity of crystallizer.

Channel between external flow guiding cylinder 4 and cylindrical central part 33 is settling section 18, inner cycle channel, settling section 18, circulation Pump 8 and pipeline 9 form outside the circular channels.Outside the circular channels are used to eliminate the elutriation of excessive fine grain and product granularity, guarantee The crystalline product that narrower particle size distribution can be produced, can sufficiently meet requirement of the client to product granularity.

Condensation part 2 includes the overflow weir from top to bottom set gradually inside condensation segment cylinder 10 and condensation segment cylinder 10 11, the first water stopping cap 12, folding pendular ring 13 and the second water stopping cap 14, condensation segment cylinder 10, overflow weir 11, the first water stopping cap 12, folding With 31 axial symmetry of central axis, condensation part 2 is located at the top of crystallization unit 1, and condensation segment cylinder for pendular ring 13 and the second water stopping cap 14 10 bottom end of body, which covers secondary steam and rises cylinder 7, is fixedly connected on the outside on taper type top 32, the lower edge of overflow weir 11 with it is cold Solidifying section cylinder 10 is tightly connected, and the top of overflow weir 11 is diametrically less than or equal to the water blocking width of the first water stopping cap 12, rolls over pendular ring 13 between the first water stopping cap 12 and the second water stopping cap 14, and the outer edge for rolling over pendular ring 13 is fixed on condensation segment cylinder 10, The internal diameter for rolling over pendular ring 13 is less than or equal to the water blocking width of the first water stopping cap 12, and the water blocking for being less than or equal to the second water stopping cap 14 is wide Degree, condensation segment cylinder 10 are equipped with coolant liquid inlet 101 in 11 position of overflow weir.

Preferably, bottom blender 6 is propeller agitator, in being advanced to the mixed solution in central draft tube 5 The evaporation interface 19 on 5 top of heart guide shell improves the interior cycle efficieny in inner cycle channel.

Preferably, the top of condensation segment cylinder 10 offers on-condensible gas outlet 102, and on-condensible gas outlet 102 In the top of overflow weir 11, the condensation segment cylinder 10 is discharged in the fixed gas in secondary steam.

Preferably, it is connected to the fine grain waterpipe 351 that disappears on the pipeline in 35 outside of clear solution outlet, to the fine grain water that will disappear It is mixed with crystallization solution, eliminates the fine grain in crystallization solution.

Preferably, 10 lower part of condensation segment cylinder offers cooling condensation mixed liquor outlet 103, and cooling condensation mixed liquor draws The height off the ground of outlet 103 is less than the height off the ground that secondary steam rises 7 steam output end of cylinder.

Preferably, condensation part 2 further includes liquid seal trough 15 and barometric pipe 16, and one end of barometric pipe 16 and cooling condense mixed liquor Outlet 103 is connected, and the other end of barometric pipe 16 accesses liquid seal trough 15, to mix the cooling condensation in condensation segment cylinder 10 Liquid is successfully led in liquid seal trough 15, and the height off the ground of fluid column is at 10 ~ 20 meters in hydraulically full in barometric pipe 16 and barometric pipe 16 Between, to make cooling condensation mixed liquor by fluid column gravity automatically into the liquid seal trough 15.

Preferably, 15 bottom of liquid seal trough offers coolant liquid and removes heating gate 151, and coolant liquid goes heating gate 151 to pass through circulation Pipeline is connected with coolant liquid inlet 101.

Preferably, the barrel dliameter of external flow guiding cylinder 4 is twice of 5 barrel dliameter of central draft tube, to fill to outside the circular channels offer Sufficient space, to eliminate excessive fine grain and eluriate the granularity of product.

Preferably, crystallization unit 1 further includes product shurry pump 17, and product shurry pump 17 is connected by pipeline with discharge port 37, Crystallization to generate crystallization unit 1 is drawn.

Preferably, vertical vacuum crystallization apparatus is plural serial stage framework, and two neighboring vertical vacuum crystallization apparatus is wherein One of circulating pump 8 outlet end wherein another 36 phase of feeding inlet with two neighboring vertical vacuum crystallization apparatus simultaneously Even.

The utility model is suitable for Solubility of Substances and varies with temperature biggish crystallisation by cooling, such as potassium chloride, ammonium sulfate The crystallization of solution, the solution (such as 90 DEG C of Klorvess Liquids) that preceding workshop section is preheating to certain temperature are being followed with fine grain outer circulation liquid is eliminated Ring pump 8 outlet mixing after, into the central draft tube 5 of crystallization unit 1 and crystallization unit 1 in suspension pushed away together by propeller agitator The evaporation interface 19 on 51 top of third end of central draft tube 5 is entered, under vacuum, solution (water) flash evaporation absorbs Heat in solution reduces temperature in solution, and solution is made to reach certain saturation degree, solutes accumulation to plane of crystal, and crystal is grown up, Bulky grain crystal is settled down to the 34 magma area of conical lower portion of crystallization unit 1 along central draft tube 5 and external flow guiding cylinder 4, passes through product The extraction of shurry pump 17 is sent into next section, and little particle continues cycling through in inner cycle channel with solution grows up, into the clear of outer circulation The solution in clear area 18, overflow enter the pipeline 9 of outside the circular channels, and the micro crystal of entrainment is disappeared brilliant water dissolution in pipeline 9, solution Under conveying by circulating pump 8, most of crystallization unit 1 that enters participates in circulation, and rest part enters next section, to guarantee this crystallization The operation liquid level of device.

The secondary steam that evaporation interface 19 generates, isolates droplet in uphill process, rises cylinder 7 by secondary steam, Into condensation part 2,11 overflow of overflow weir and under coolant liquid by the first water stopping cap 12, folding pendular ring 13, the second water stopping cap 14 Three coolant liquid curtains (cascade) are formed, it is not condensed after secondary steam and the three condensations curtain of night (cascade) come into full contact with condensation Fixed gas is drawn from top on-condensible gas outlet 102, after separating entrained drop, into vacuum system, is discharged into atmosphere. Coolant liquid can be the low temperature mother liquor after slurry separation, and the end effect vertical vacuum crystallization apparatus of plural serial stage crystallization is because of evaporating temperature Lower, secondary steam waste heat recovery value is little, commonly uses circulating water.Coolant liquid and the condensed mixed liquor of secondary steam are logical Supercooling condensation 103 overflow of mixed liquor outlet enters barometric pipe 16, into liquid seal trough 15, send the preceding paragraph to make by circulating line cold But liquid, or for preparing solution.

The utility model is the vapor partial pressure that solution in solution is reduced using vacuum, evaporates solution and takes away heat, real It is to generate saturation degree by concentration and cooling two kinds of effects simultaneously in matter, makes solute crystals nucleation, growth.It is strong compared to other The advantages of compeling crystallizer (such as FC, OLSO type crystallizer) of outer circulation are as follows: main equipment is simple, is not required to heat exchanger, and there is no interior Problem is cleared up in surface serious scale and fouling, to influence production capacity；Vacuumizing pressure is close with solution vapor partial pressure, It operates more stable.

Crystallization unit 1 and condensation part 2 are combined into an equipment by the utility model, the crystallization unit 1 of difference and other forms with Condensation part 2 is separated, major advantage: not needing that secondary steam is introduced condensation part from crystallization unit with pipeline, shortens secondary Vapor flow path is eliminated because the resistance of ducting causes secondary steam to overheat, and increases cooling liquid measure；It eliminates and increases because of pipeline connection The seal point leakage added, and increase the sucking rate of vacuum system；The evaporating temperature that solution balances each other with vacuum is also reduced simultaneously, The evaporation capacity for improving solution, has saved power energy consumption.Equipment investment is saved, it may be assumed that saved crystallization unit 1 and condensation part 2 Pipeline；It has saved condensation part 2 and backing material is installed；Save the space of equipment installation.

Central draft tube 5, bottom blender 6 and external flow guiding cylinder 4 are set in the crystallization unit of the utility model, and it is logical to form interior circulation Road, advantage are main are as follows: high saturation region in crystallization unit 1 is eliminated, saturation degree is relatively uniform everywhere in crystallization unit 1, and compared with Low (degree of supercooling can control at < 1 DEG C), improves evaporation intensity, enhances the production capacity of crystallization unit 1；Propeller agitator is answered With improving interior cycle efficieny, reduce crystal and propeller agitator blade and collide broken nucleation probability.Propeller agitator Using frequency control, it is more conducive to adjustment produce load.

The setting advantage of the outside the circular channels of the utility model: washing in a pan for excessive fine grain and product granularity is eliminated It washes, guarantees the product for producing Unusually narrow particle size distribution, granularity can be produced up to the big grain size product of 600~1200umr, sufficiently met Requirement of the user to product crystallization different grain size distribution.It selects the axial-flow pump of big flow low lift as circulating pump 8, effectively improves Outer circulation amount, is more conducive to the elutriation of crystal size and the control of crystal ownership.It mixes and takes out relative to mix suspending (MSMPR) crystallizer can make the effective volume of crystallization unit 1 reduce by 30% or more, save the investment of equipment.

The applicability of the utility model is wide, and it is more to can be used for being insulated cooling method, evaporation, contact method and reaction method etc. Kind crystallization is more suitable for large-scale industry crystallization production.

The utility model is described by above-mentioned related embodiment, however above-described embodiment is only to implement the utility model Example.It must be noted that the embodiment disclosed is not limiting as the scope of the utility model.On the contrary, not departing from this It is changed and retouched made by the spirit and scope of utility model, belongs to the scope of patent protection of the utility model.

Claims (10)

1. a kind of vertical vacuum crystallization apparatus, characterized by comprising: crystallization unit and condensation part；

The crystallization unit includes crystallized region cylinder, external flow guiding cylinder, central draft tube, bottom blender, secondary steam rising cylinder, circulation Pump, inner cycle channel and outside the circular channels；

The crystallized region cylinder is the axially symmetric structure with central axis, including be sequentially connected taper type top, in straight tube shape Portion and conical lower portion, include top and bottom in the middle part of the straight tube shape, the big circular bottom surface on the taper type top and it is described on End is connected, and the bottom surface of the conical lower portion is connected with the lower end, and it is molten that the middle position in the middle part of the straight tube shape offers clarification Liquid outlet symmetrically offers feeding inlet and discharge port using the central axis as symmetry axis in the conical lower portion；

The external flow guiding cylinder includes opposite first end and second end, and the external flow guiding cylinder is located at the interior of the crystallized region cylinder Portion, and the first end is joined in the middle part of the variable diameter and the straight tube shape by being fixedly connected in the middle part of variable diameter and the straight tube shape Place is located at the top of the clear solution outlet, and the lower end in the middle part of the second end and the straight tube shape is in same horizontal line On, the external flow guiding cylinder is with the central axis axial symmetry；

The central draft tube includes opposite third end and the 4th end, and the central draft tube is located at the interior of the external flow guiding cylinder Portion, and the horizontal plane where the third end is higher than the position that the external flow guiding cylinder intersects with straight tube shape middle part, described the The liquid level at three ends top is evaporation interface, and the 4th end is lower than the second end in the height of horizontal plane in the height of horizontal plane Degree, the central draft tube is with the central axis axial symmetry；

The bottom blender is located at the inside at the 4th end；

The secondary steam rises cylinder and is cylindrical structure and is connected with the top on the taper type top and with the central axis Axial symmetry；

The circulating pump is located at the outside of the crystallized region cylinder, and is drawn by pipeline and the feeding inlet and the clear solution Outlet is connected；

In the cylinder of the central draft tube and channel between the external flow guiding cylinder and the central draft tube is formed in described Circulation canal；

Channel between the external flow guiding cylinder and the cylindrical central part is settling section, the inner cycle channel, the settling section, The circulating pump and the pipeline form the outside the circular channels；

The condensation part includes condensation segment cylinder and the condensation segment inner barrel is from top to bottom set gradually overflow weir, One water stopping cap, folding pendular ring and the second water stopping cap, the condensation segment cylinder, the overflow weir, first water stopping cap, the folding liquid With the central axis axial symmetry, the condensation part is located at the top of the crystallization unit, and institute for ring and second water stopping cap It states condensation segment cylinder bottom cap residence and states the outside that secondary steam rising cylinder is fixedly connected on the taper type top, the overflow The lower edge on weir and the condensation segment cylinder are tightly connected, and the top of the overflow weir is diametrically less than or equal to first water blocking The water blocking width of cap, the folding pendular ring is between first water stopping cap and second water stopping cap, and the folding pendular ring Outer edge is fixed on the condensation segment cylinder, and the water blocking that the internal diameter of the folding pendular ring is less than or equal to first water stopping cap is wide Degree, and it is less than or equal to the water blocking width of second water stopping cap, the condensation segment cylinder is equipped with cooling in the overflow weir position Liquid inlet.

2. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the bottom blender is propeller agitator, The evaporation interface the mixed solution in the central draft tube is advanced to the central draft tube top follows in making Interior cycle efficieny in ring channel improves.

3. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the top of the condensation segment cylinder offers On-condensible gas outlet, the on-condensible gas outlet are located at the top of the overflow weir, to by not coagulating in secondary steam The condensation segment cylinder is discharged in gas.

4. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the pipe on the outside of the clear solution outlet It is connected to the fine grain waterpipe that disappears on road, is mixed fine grain water will be disappeared with crystallization solution, eliminates the fine grain in crystallization solution.

5. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that condensation segment cylinder lower part offers cold But mixed liquor outlet is condensed, the height off the ground of the cooling condensation mixed liquor outlet is less than secondary steam rising cylinder and goes out The height off the ground at vapour end.

6. vertical vacuum crystallization apparatus as claimed in claim 5, it is characterised in that the condensation part further includes liquid seal trough and big Air leg, one end of the barometric pipe are connected with the cooling condensation mixed liquor outlet, and the other end of the barometric pipe accesses institute Liquid seal trough is stated, it is described big successfully to lead to the condensation segment cylinder intracorporal cooling condensation mixed liquor in the liquid seal trough The height off the ground of fluid column is between 10 ~ 20 meters in the hydraulically full and described barometric pipe in air leg, to make cooling condensation mixed liquor By fluid column gravity automatically into the liquid seal trough.

7. vertical vacuum crystallization apparatus as claimed in claim 6, it is characterised in that the fluid-tight trench bottom offers coolant liquid Heating gate is removed, the coolant liquid goes heating gate to be connected by circulating line with the coolant liquid inlet.

8. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the barrel dliameter of the external flow guiding cylinder is in described Twice of heart guide shell barrel dliameter is produced to provide adequate space to the outside the circular channels with eliminating excessive fine grain and eluriating The granularity of product.

9. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the crystallization unit further includes product shurry pump, The product shurry pump is connected by pipeline with the discharge port, and the crystallization to generate the crystallization unit is drawn.

10. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that the vertical vacuum crystallization apparatus is multistage Series architecture, the outlet end of the circulating pump of one of two neighboring vertical vacuum crystallization apparatus simultaneously with it is two neighboring vertical Wherein another feeding inlet of vacuum crystallization device is connected.