CN108714311A - A kind of vertical vacuum crystallization apparatus - Google Patents
A kind of vertical vacuum crystallization apparatus Download PDFInfo
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- CN108714311A CN108714311A CN201810827841.8A CN201810827841A CN108714311A CN 108714311 A CN108714311 A CN 108714311A CN 201810827841 A CN201810827841 A CN 201810827841A CN 108714311 A CN108714311 A CN 108714311A
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
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Abstract
The present invention 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, indirect steam rising cylinder, circulating pump, inner cycle channel and outside the circular channels；Condensation part includes condensation segment cylinder and downflow 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；It is an advantage of the invention 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, and operation is more stable.Crystallization unit and condensation part are combined into an equipment, shorten indirect steam flow path, eliminate that increased seal point leaks because pipeline connect.Inner cycle channel eliminates high saturation region in crystallization unit, and saturation degree is relatively uniform and relatively low everywhere, and outside the circular channels eliminate excessive fine grain, while eluriating out the product of Unusually narrow particle size distribution.
Description
Technical field
The present invention relates to chemical separating fields, and in particular to a kind of vertical vacuum crystallization apparatus.
Background technology
Crystallization refers to the process of that solid is precipitated with crystal state from gas, liquid or fusant, this process is by heating power
What and kinetic factor determined, solute will be precipitated from solution, it is necessary to constantly obtain energy from outside, make solution in solution
Constantly evaporation reaches saturation and supersaturation, when solution is not up to saturated（In stable region）, solute not will produce crystallization,
When solution is between solubility curve and supersolubility curve（Metastable zone）, lolute crystallization and dissolving 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 easily by ectocine, 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 secondary nucleation existing for crystal, during industrial crystallization, usually control secondary nucleation, i.e. fluid
Shear stress is nucleated and Crystallisation, that is, selects suitable stirring pattern and rotating speed.
According to the universal diffusion theory analysis of chemical engineering unit operation, the growth of crystal is related with following factor：
（1）The motive force of crystal growth is the supersaturation concentration difference and transmission speed of solution, the solutes accumulation in supersaturated solution
Opposing stationary liquid layer near to nucleus, and reach plane of crystal across opposing stationary solution layer and be embedded in crystal face, keep its crystal long
Greatly, and crystallization heat is released, heat is transmitted to by diffusion in solution again.
（2）The temperature of solution, at the same time 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 larger crystal of grain 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 determines 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, crystal fracture is caused to increase at the possibility of 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
Profit, 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 is tied with leaving
After the magma mixing of brilliant room bottom, from pumping toward heating room.Magma does not occur the indoor heating of heating (being usually 2 ~ 6 DEG C)
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 due to device without mixing inside the crystallizer so that the degree of mixing of slurry is deteriorated, and leads to the broad particle distribution of product；And
Since there are outer circulation coolings in the equipment, so its cooling tube can be easier fouling.
Invention content
To solve the above problems, the present invention proposes a kind of vertical vacuum crystallization apparatus.
The technical scheme is that：A kind of vertical vacuum crystallization apparatus, it is characterised in that including:Crystallization unit and condensation
Portion；
The crystallization unit includes crystallized region cylinder, external flow guiding cylinder, central draft tube, bottom blender, indirect steam rising cylinder, cycle
Pump, inner cycle channel and outside the circular channels；
The crystallized region cylinder is the axially symmetric structure for having central shaft, 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 with 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 centre position in the middle part of the straight tube shape offers clarification
Liquid outlet symmetrically offers feeding mouth and discharge port using the central shaft 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, by being fixedly connected in the middle part of reducing and the straight tube shape, the reducing joins in the middle part of the straight tube shape
Place is positioned at the top of the clear solution outlet, and the second end is with the lower end in the middle part of the straight tube shape in same horizontal line
On, the external flow guiding cylinder is with the central shaft 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 and the straight tube shape middle part are intersected, described the
The liquid level at three ends top be evaporation interface, the 4th end horizontal plane height less than the second end horizontal plane height
Degree, the central draft tube is with the central shaft axial symmetry；
The bottom blender is located at the inside at the 4th end；
The indirect steam rises cylinder and is cylindrical structure and is connected with the top on the taper type top and with the central shaft
Axial symmetry；
The circulating pump is located at the outside of the crystallized region cylinder, and is drawn by pipeline and the feeding mouth 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 downflow weir,
One water stopping cap, folding pendular ring and the second water stopping cap, the condensation segment cylinder, the downflow weir, first water stopping cap, the folding liquid
With the central shaft 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 the second steam rising cylinder is fixedly connected on the taper type top, the overflow
The lower edge on weir is tightly connected with the condensation segment cylinder, and the top of the downflow 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 internal diameter of the folding pendular ring is wide less than or equal to the water blocking of first water stopping cap
Degree, and less than or equal to the water blocking width of second water stopping cap, the condensation segment cylinder is equipped with cooling in the downflow weir position
Liquid inlet.
Preferably, the bottom blender is propeller agitator, to push away the mixed solution in the central draft tube
Entering the evaporation interface on the central draft tube top makes the interior cycle efficieny in inner cycle channel improve.
Preferably, the top of the condensation segment cylinder offers on-condensible gas outlet, on-condensible gas outlet position
In the top of the downflow weir, the condensation segment cylinder is discharged in the fixed gas in indirect 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 indirect 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 is condensed with the cooling
Mixed liquor outlet is connected, and the other end of the barometric pipe accesses the liquid seal trough, to will be cold in the condensation segment cylinder
But condensation mixed liquor is successfully led in the liquid seal trough, in hydraulically full in the barometric pipe and 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 goes heating gate, the coolant liquid that heating gate is gone to pass through cycle
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 the circulating pump of one of them while wherein another feeding mouth phase with two neighboring vertical vacuum crystallization apparatus
Even.
Compared with prior art, a kind of vertical vacuum crystallization apparatus main equipment of the invention is simple, is not required to heat exchanger, no
There are inner surface serious scales and fouling to clear up problem, to influence production capacity；Vacuumizing pressure is divided with solution vapor
Close, operation is more stable.Crystallization unit and condensation part are combined into an equipment, are different from the crystallizing evaporator of other forms and cold
Condenser is separated, and major advantage is：Indirect steam need not be introduced into condensation part from crystallization unit with pipeline, shorten secondary steaming
Steam flow road is eliminated because the resistance of ducting causes indirect steam to overheat, and increases cooling liquid measure；It eliminates and increases because pipeline connects
Seal point leakage, and increase the rate of air sucked in required of vacuum system；The evaporating temperature that solution balances each other with vacuum is also reduced simultaneously, is carried
The high evaporation capacity of solution, has saved power energy consumption, while having saved equipment investment.The inner cycle channel of the present invention eliminates crystallization
High saturation region in device, saturation degree is relatively uniform and relatively low everywhere in crystallizer, improves evaporation intensity, reinforcing finishes
The production capacity of brilliant device, propeller agitator application improve interior cycle efficieny, reduce crystal and the broken nucleation of blade collision
Probability, blender use frequency control, are more conducive to adjustment produce load；Outside the circular channels eliminate excessive fine grain, and
The elutriation of product granularity guarantees the product for producing Unusually narrow particle size distribution.
Description of the drawings
Fig. 1 is a kind of overall structure diagram of vertical vacuum crystallization apparatus of the present invention.
Specific implementation mode
To make to have further understanding to the purpose of the present invention, construction, feature and its function, hereby coordinate embodiment detailed
It is described as follows.
Referring to Fig. 1, Fig. 1 is a kind of vertical vacuum crystallization apparatus overall structure diagram of the present invention, as shown in Figure 1,
The vertical vacuum crystallization apparatus of one embodiment of the 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, indirect steam rising cylinder
7, circulating pump 8, inner cycle channel and outside the circular channels.
Crystallized region cylinder 3 is the axially symmetric structure for having central shaft 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 centre position offers clear in the middle part of straight tube shape
Clear solution outlet 35 with central shaft 31 is symmetry axis in conical lower portion 34, symmetrically offers feeding mouth 36 and discharge port 37.
Taper type top 32 is concentrated for indirect 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 reducing 43 in the middle part of straight tube shape 33, reducing 43 is located at clarification with 33 junctions in the middle part of straight tube shape
The top of solution outlet 35, in the same horizontal line with lower end 332, external flow guiding cylinder 4 is with 31 axial symmetry of central shaft for second end 42.
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 33 positions intersected in the middle part of external flow guiding cylinder 4 and straight tube shape, 51 top of third end
Liquid level is evaporation interface 19, and the 4th end 52 is less than second end 42 in the height of horizontal plane, central draft tube 5 in the height of horizontal plane
With 31 axial symmetry of central shaft.Bottom blender 6 is located at the inside at the 4th end 52.
Indirect 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 shaft
Claim.
Circulating pump 8 is located at the outside of crystallized region cylinder 3, and passes through pipeline 9 and feeding mouth 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 relatively low 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, cycle
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, ensure
The crystalline product that narrower particle size distribution can be produced, can fully meet requirement of the client to product granularity.
Condensation part 2 includes the downflow 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, downflow weir 11, the first water stopping cap 12, folding
With 31 axial symmetry of central shaft, 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 the second steam and rises cylinder 7, is fixedly connected on the outside on taper type top 32, the lower edge of downflow weir 11 with it is cold
Solidifying section cylinder 10 is tightly connected, and the top of downflow 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 wide less than or equal to the water blocking of the second water stopping cap 14
Degree, condensation segment cylinder 10 are equipped with coolant liquid inlet 101 in 11 position of downflow 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 makes the interior cycle efficieny in inner cycle channel improve.
Preferably, the top of condensation segment cylinder 10 offers on-condensible gas outlet 102, on-condensible gas outlet 102
In the top of downflow weir 11, the condensation segment cylinder 10 is discharged in the fixed gas in indirect 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 indirect 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 condenses mixed liquor with cooling
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 goes heating gate 151, coolant liquid that heating gate 151 is gone to pass through cycle
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 be filled 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 mouth with two neighboring vertical vacuum crystallization apparatus simultaneously
Even.
The present invention varies with temperature larger crystallisation by cooling, such as potassium chloride, ammonium sulfate solution suitable for Solubility of Substances
Crystallization, preceding workshop section is preheating to the solution of certain temperature（Such as 90 DEG C of Klorvess Liquids）With elimination fine grain outer circulation liquid in circulating pump
8 outlet mixing after, into the central draft tube 5 of crystallization unit 1 and crystallization unit 1 in suspension be advanced to together by propeller agitator
The evaporation interface 19 on 51 top of third end of central draft tube 5, under vacuum, solution（Water）Flash evaporation, absorbent solution
Middle heat reduces temperature in solution, and solution is made to reach certain saturation degree, solutes accumulation to plane of crystal, and crystal is grown up, big
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 slurry
17 extraction of pump is sent into next section, and little particle, which is continued cycling through with solution in inner cycle channel, grows up, into the settling section of outer circulation
18 solution, overflow enter the pipeline 9 of outside the circular channels, and the micro crystal of entrainment is disappeared brilliant water dissolution in pipeline 9, and solution passes through
Under the conveying of circulating pump 8, most of crystallization unit 1 that enters participates in cycle, and rest part enters next section, to ensure this crystallizer
Operate liquid level.
The indirect steam that evaporation interface 19 generates, isolates droplet in uphill process, rises cylinder 7 by indirect steam,
Into condensation part 2,11 overflow of downflow weir and under coolant liquid by the first water stopping cap 12, folding pendular ring 13, the second water stopping cap 14
Form three coolant liquid curtains（Cascade）, indirect steam and three condensation the curtains of night（Cascade）After coming into full contact with condensation, it is not condensed
Fixed gas is drawn from top on-condensible gas outlet 102, after detaching entrained drop, into vacuum system, is discharged into air.
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
Relatively low, indirect steam waste heat recovery value is little, commonly uses circulating water.Coolant liquid is logical with the condensed mixed liquor of indirect steam
103 overflow of supercooling condensation 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 present invention is that the vapor partial pressure of solution in solution is reduced using vacuum, so that solution is evaporated and takes away heat, substantially
It is to generate saturation degree by concentration and cooling two kinds of effects simultaneously, makes solute crystals nucleation, growth.It is forced outer compared to other
The advantages of crystallizer (such as FC, OLSO type crystallizer) of cycle is：Main equipment is simple, is not required to heat exchanger, and inner surface is not present
Problem is cleared up in serious scale and fouling, to influence production capacity；Vacuumizing pressure divides close, operation with solution vapor
It is more stable.
Crystallization unit 1 and condensation part 2 are combined into an equipment, crystallization unit 1 and condensation of the difference with other forms by the present invention
Portion 2 is separated, major advantage：Indirect steam need not be introduced into condensation part from crystallization unit with pipeline, shorten indirect steam
Flow path is eliminated because the resistance of ducting causes indirect steam to overheat, and increases cooling liquid measure；It eliminates because that pipeline connects is increased
Seal point leaks, and increases the rate of air sucked in required of vacuum system；The evaporating temperature that solution balances each other with vacuum is also reduced simultaneously, is improved
The evaporation capacity of solution, has saved power energy consumption.Equipment investment is saved, i.e.,：The pipeline of crystallization unit 1 and condensation part 2 is saved；
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 present invention, forms inner cycle channel,
Its advantage is mainly：High saturation region in crystallization unit 1 is eliminated, saturation degree is relatively uniform and relatively low everywhere in crystallization unit 1
（Degree of supercooling can control<1℃）, evaporation intensity is improved, the production capacity of crystallization unit 1 is enhanced；Propeller agitator application,
Interior cycle efficieny is improved, crystal is reduced and is crushed nucleation probability with the collision of propeller agitator blade.Propeller agitator is adopted
With frequency control, it is more conducive to adjustment produce load.
The setting advantage of the outside the circular channels of the present invention:The elutriation of excessive fine grain and product granularity is eliminated, is protected
Card can produce the product of Unusually narrow particle size distribution, can produce granularity up to the big grain size products of 600~1200umr, fully meet user couple
Product crystallizes the requirement of different grain size distribution.It selects the axial-flow pump of big flow low lift as circulating pump 8, effectively increases outer follow
Circular rector is more conducive to the control of the elutriation and crystal ownership of crystal size.It mixes and takes out relative to mix suspending（MSMPR）Knot
Brilliant device can make the effective volume of crystallization unit 1 reduce by 30% or more, save the investment of equipment.
The applicability of the present invention is wide, can be used for a variety of knots such as adiabatic cooling method, evaporation, contact method and reaction method
Crystalline substance is more suitable for large-scale industry crystallization production.
The present invention is described by above-mentioned related embodiment, however above-described embodiment is only the example for implementing the present invention.
It must be noted that the embodiment disclosed is not limiting as the scope of the present invention.On the contrary, do not depart from the present invention spirit and
It is changed and retouched made by range, belongs to the scope of patent protection of the present invention.
Claims (10)
1. a kind of vertical vacuum crystallization apparatus, it is characterised in that including:Crystallization unit and condensation part；
The crystallization unit includes crystallized region cylinder, external flow guiding cylinder, central draft tube, bottom blender, indirect steam rising cylinder, cycle
Pump, inner cycle channel and outside the circular channels；
The crystallized region cylinder is the axially symmetric structure for having central shaft, 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 with 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 centre position in the middle part of the straight tube shape offers clarification
Liquid outlet symmetrically offers feeding mouth and discharge port using the central shaft 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, by being fixedly connected in the middle part of reducing and the straight tube shape, the reducing joins in the middle part of the straight tube shape
Place is positioned at the top of the clear solution outlet, and the second end is with the lower end in the middle part of the straight tube shape in same horizontal line
On, the external flow guiding cylinder is with the central shaft 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 and the straight tube shape middle part are intersected, described the
The liquid level at three ends top be evaporation interface, the 4th end horizontal plane height less than the second end horizontal plane height
Degree, the central draft tube is with the central shaft axial symmetry；
The bottom blender is located at the inside at the 4th end；
The indirect steam rises cylinder and is cylindrical structure and is connected with the top on the taper type top and with the central shaft
Axial symmetry；
The circulating pump is located at the outside of the crystallized region cylinder, and is drawn by pipeline and the feeding mouth 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 downflow weir,
One water stopping cap, folding pendular ring and the second water stopping cap, the condensation segment cylinder, the downflow weir, first water stopping cap, the folding liquid
With the central shaft 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 the second steam rising cylinder is fixedly connected on the taper type top, the overflow
The lower edge on weir is tightly connected with the condensation segment cylinder, and the top of the downflow 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 internal diameter of the folding pendular ring is wide less than or equal to the water blocking of first water stopping cap
Degree, and less than or equal to the water blocking width of second water stopping cap, the condensation segment cylinder is equipped with cooling in the downflow 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 to be 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 downflow weir, to by not coagulating in indirect 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
The fine grain waterpipe that disappears is connected on road, fine grain water is mixed with crystallization solution will disappear, and 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 indirect 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 cooling condensation mixed liquor in the condensation segment cylinder in the liquid seal trough
The height off the ground of fluid column is between 10 ~ 20 meters in the hydraulically full and 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
Go heating gate, the coolant liquid that heating gate is gone to be connected with the coolant liquid inlet by circulating line.
8. vertical vacuum crystallization apparatus as described in claim 1, it is characterised in that during the barrel dliameter of the external flow guiding cylinder is described
Twice of heart guide shell barrel dliameter is produced to give the outside the circular channels to provide adequate space 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 mouth of vacuum crystallization device is connected.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
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| CN201810827841.8A CN108714311A (en) | 2018-07-25 | 2018-07-25 | A kind of vertical vacuum crystallization apparatus |
| PCT/CN2018/111214 WO2020019542A1 (en) | 2018-07-25 | 2018-10-22 | Vertical vacuum crystallizing apparatus |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201810827841.8A CN108714311A (en) | 2018-07-25 | 2018-07-25 | A kind of vertical vacuum crystallization apparatus |
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| CN201810827841.8A Pending CN108714311A (en) | 2018-07-25 | 2018-07-25 | A kind of vertical vacuum crystallization apparatus |
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| Country | Link |
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| CN (1) | CN108714311A (en) |
| WO (1) | WO2020019542A1 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109603189A (en) * | 2018-12-22 | 2019-04-12 | 江苏新宏大集团有限公司 | W type end socket, the crystallizer with W type end socket and W type takeshapes of closure mode |
| CN112237751A (en) * | 2019-07-16 | 2021-01-19 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization device with automatic crystal scale processing function |
| CN113184907A (en) * | 2021-05-31 | 2021-07-30 | 河钢承德钒钛新材料有限公司 | Method for purifying sodium chromate |
| CN115385407A (en) * | 2022-07-20 | 2022-11-25 | 中科嘉辞(昆山)环保科技有限公司 | Industrial wastewater zero-discharge clear liquid anti-blocking type crystallization evaporator |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1757599A (en) * | 2005-11-03 | 2006-04-12 | 湖南百利工程科技有限公司 | Method for producing ammonium sulfate |
| CN101531382A (en) * | 2008-12-29 | 2009-09-16 | 卫宏远 | Production process and crystallization device for large-particle ammonium sulfate |
| CN203763891U (en) * | 2014-03-03 | 2014-08-13 | 成都深蓝高新技术发展有限公司 | Vacuum low-temperature evaporating crystallizer |
| CN104386710A (en) * | 2014-10-22 | 2015-03-04 | 北京华福工程有限公司 | Device and method for producing ammonium sulfate |
| CN205482424U (en) * | 2016-03-17 | 2016-08-17 | 惠州景华包装制品有限公司 | Vacuum condensing system |
| CN107648879A (en) * | 2017-10-30 | 2018-02-02 | 中盐工程技术研究院有限公司 | One kind crystallization condensation integrated device |
| CN208711101U (en) * | 2018-07-25 | 2019-04-09 | 江苏新宏大集团有限公司 | A kind of vertical vacuum crystallization apparatus |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102008029050A1 (en) * | 2008-06-18 | 2009-12-24 | Gea Messo Gmbh | Process and apparatus for the continuous production of a crystallizate with constant particle size distribution |
-
2018
- 2018-07-25 CN CN201810827841.8A patent/CN108714311A/en active Pending
- 2018-10-22 WO PCT/CN2018/111214 patent/WO2020019542A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1757599A (en) * | 2005-11-03 | 2006-04-12 | 湖南百利工程科技有限公司 | Method for producing ammonium sulfate |
| CN101531382A (en) * | 2008-12-29 | 2009-09-16 | 卫宏远 | Production process and crystallization device for large-particle ammonium sulfate |
| CN203763891U (en) * | 2014-03-03 | 2014-08-13 | 成都深蓝高新技术发展有限公司 | Vacuum low-temperature evaporating crystallizer |
| CN104386710A (en) * | 2014-10-22 | 2015-03-04 | 北京华福工程有限公司 | Device and method for producing ammonium sulfate |
| CN205482424U (en) * | 2016-03-17 | 2016-08-17 | 惠州景华包装制品有限公司 | Vacuum condensing system |
| CN107648879A (en) * | 2017-10-30 | 2018-02-02 | 中盐工程技术研究院有限公司 | One kind crystallization condensation integrated device |
| CN208711101U (en) * | 2018-07-25 | 2019-04-09 | 江苏新宏大集团有限公司 | A kind of vertical vacuum crystallization apparatus |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109603189A (en) * | 2018-12-22 | 2019-04-12 | 江苏新宏大集团有限公司 | W type end socket, the crystallizer with W type end socket and W type takeshapes of closure mode |
| CN112237751A (en) * | 2019-07-16 | 2021-01-19 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization device with automatic crystal scale processing function |
| CN113184907A (en) * | 2021-05-31 | 2021-07-30 | 河钢承德钒钛新材料有限公司 | Method for purifying sodium chromate |
| CN115385407A (en) * | 2022-07-20 | 2022-11-25 | 中科嘉辞(昆山)环保科技有限公司 | Industrial wastewater zero-discharge clear liquid anti-blocking type crystallization evaporator |
| CN115385407B (en) * | 2022-07-20 | 2024-01-12 | 中科嘉辞(昆山)环保科技有限公司 | Industrial wastewater zero-emission clear liquid anti-blocking crystallization evaporator |
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| Publication number | Publication date |
|---|---|
| WO2020019542A1 (en) | 2020-01-30 |
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