CN204034311U - A kind of spiral-flow type fluidized-bed crystallizer - Google Patents
A kind of spiral-flow type fluidized-bed crystallizer Download PDFInfo
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- CN204034311U CN204034311U CN201420460547.5U CN201420460547U CN204034311U CN 204034311 U CN204034311 U CN 204034311U CN 201420460547 U CN201420460547 U CN 201420460547U CN 204034311 U CN204034311 U CN 204034311U
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Abstract
A kind of spiral-flow type fluidized-bed crystallizer, comprise a body, described bed body is the assembly of cylinder and conic tube, the internal diameter of the large end of conic tube is identical with the internal diameter of cylinder, the vertex of a cone of conic tube is arc-shaped, and conic tube is positioned at the below of cylinder, and its large end is connected with the lower end of cylinder; The upper end closed of cylinder, the end face of cylinder upper end is provided with crystal seed and adds entrance, conic tube lower section sidewall is provided with the feed pipe adding feed liquid, described feed pipe is at least two, be uniformly distributed around conic tube sustained height, each feed pipe is all positioned at the horizontal tangent direction of conic tube, the vertex of a cone of conic tube lower end is provided with crystal outlet, the upper portion side wall of cylinder is provided with the discharge nozzle exporting mother liquor, and described discharge nozzle is positioned at the horizontal tangent direction of cylinder and the outlet of discharge nozzle is consistent with the eddy flow rotation direction that feed liquid is formed.In order to meet the requirement of gap crystallization processes, cooling jacket can be set on the basis of said structure.
Description
Technical field
The utility model patent belongs to the crystallization technique field of Chemical Engineering, relates to a kind of crystallizer.
Background technology
Crystallization is a unit operations in chemical products preparation, stirring tank crystallizer is the crystallizer generally used, because the stirrer paddle of this type of crystallizer has strong fragmentation to crystal, thus secondary nucleation speed is high, crystalline product particle diameter is little, size distribution is wide, and crystal morphology is poor, is difficult to the requirement meeting some chemical products.
Theoretically, obtain the crystalline product that epigranular, crystalline form are neat, it is crucial for controlling secondary nucleation.For this reason, there are researchers that fluidization technology is used for crystallization process, to avoid stirrer paddle to the fragmentation of crystal and to reduce secondary nucleation speed.As have studied the application of spouted fluidized bed at crystallization process in the paper " in spouted fluidized bed the research of sandy aluminium hydroxide crystallization experiment " that the people such as Zhao Kun deliver (see " Sichuan is metallurgical ", 33 volumes the 2nd phase, 63 ~ 66 pages), but this crystallization fluid bed is confined to traditional fluidization process, the inner turbulence of bed is violent, secondary nucleation is still comparatively strong, and the crystalline form of crystalline product and size distribution are still undesirable.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, provides a kind of spiral-flow type fluidized-bed crystallizer, to reduce the secondary nucleation speed in crystallization process, increases the particle diameter of crystalline product, and makes crystalline product narrow particle size distribution, pattern neat.
Spiral-flow type fluidized-bed crystallizer described in the utility model, comprise a body, described bed body is the assembly of cylinder and conic tube, the internal diameter of the large end of conic tube is identical with the internal diameter of cylinder, the vertex of a cone of conic tube is arc-shaped, conic tube is positioned at the below of cylinder, and its large end is connected with the lower end of cylinder, the upper end closed of cylinder, the end face of cylinder upper end is provided with crystal seed and adds entrance, conic tube lower section sidewall is provided with the feed pipe adding feed liquid, described feed pipe is at least two, be uniformly distributed around conic tube sustained height, each feed pipe is all positioned at the horizontal tangent direction of conic tube, added feed liquid is made to form eddy flow, the vertex of a cone of conic tube lower end is provided with crystal outlet, the upper portion side wall of cylinder is provided with the discharge nozzle exporting mother liquor, described discharge nozzle is positioned at the horizontal tangent direction of cylinder and the outlet of discharge nozzle is consistent with the eddy flow rotation direction that feed liquid is formed.
In order to better realize goal of the invention, spiral-flow type fluidized-bed crystallizer described in the utility model have selected following structural parameters:
1, the height L of conic tube
1=(0.5 ~ 1.2) D, the height L of cylinder
2=(1 ~ 5) D, described D is the internal diameter of cylinder, and the internal diameter D of cylinder mainly determines according to the volume crystalline rate of crystallizing system and the production capacity of crystallizer.
Distance L between the vertex of a cone outer wall of 2, feed liquid feed pipe center line and conic tube
3=(0.3 ~ 0.5) L
1, described L
1for the height of conic tube.
3, the center line of crystal outlet and the angle α of bed body center line are 30 ° ~ 45 °.
In order to meet the requirement of batch crystallization process, can arrange cooling jacket on the basis of said structure, described cooling jacket is arranged around the external wall of bed, and there is cooling water inlet its underpart, and coolant outlet is arranged at its top.
The operation principle of spiral-flow type fluidized-bed crystallizer described in the utility model: crystal seed adds from crystallizer top, feed liquid tangentially enters from the tapered sidewalls of crystallizer bottom, mother liquor is tangentially discharged from top cylinder sidewall, form slow screw type rotary flowing (see Fig. 5) upwards, suspended crystal circles under the effect of eddy flow feed liquid, and continuous crystal growth, when crystal grow up can not balance self gravitation to suspending power time, the bottom of falling crystallizer voluntarily draws off from crystal outlet; The mother liquor of discharging from crystallizer top, supplements and exchange heat through fresh feed liquid, reaches required degree of supersaturation, turned back to the feed pipe of crystallizer by circulating pump, realize the circulation of feed liquid.
The utility model has following beneficial effect:
1, because feed liquid forms slow screw type rotary flowing upwards in the bed body of crystallizer described in the utility model, suspended crystal circles around bed body axis, and in crystal growth process, there is no the strong impaction of stirrer paddle, thus uniform crystal dispersion crystal growth in feed liquid, can not be chipping, the speed of secondary nucleation greatly weakens, and the grain number of gained crystal product is close with the grain number dropping into crystal seed, narrow particle size distribution, pattern neat (see embodiment).
2, crystallizer described in the utility model and miscellaneous equipment combine, and can meet the requirement of periodic crystallisation and continuous crystallisation technique.
Without any component in the bed body of 3, crystallizer described in the utility model, thus not easily blockage phenomenon, stable work in work.
4, mold structure described in the utility model is simple, and be easy to processing and fabricating, thus investment cost is few, is conducive to promoting the use of.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of spiral-flow type fluidized-bed crystallizer described in the utility model;
Fig. 2 is the top view of Fig. 1;
Fig. 3 is the A-A profile of Fig. 1;
Fig. 4 is another structural representation of spiral-flow type fluidized-bed crystallizer described in the utility model, is provided with cooling jacket;
Fig. 5 is the fundamental diagram of spiral-flow type fluidized-bed crystallizer described in the utility model;
Fig. 6 is a kind of periodic crystallisation system that spiral-flow type fluidized-bed crystallizer described in the utility model and miscellaneous equipment are combined into;
Fig. 7 is a kind of continuous crystallizing system that spiral-flow type fluidized-bed crystallizer described in the utility model and miscellaneous equipment are combined into;
Fig. 8 is the experimental provision system diagram of spiral-flow type fluidized-bed crystallizer described in the utility model for potassium dihydrogen phosphate crystallization.
In figure, 1-conic tube, 2-cylinder, the feed pipe of 3-feed liquid, the discharge nozzle of 4-output mother liquor, 5-crystal exports, and 6-crystal seed adds entrance, 7-cooling water inlet, 8-coolant outlet, 9-cooling jacket, 10-spiral-flow type fluidized-bed crystallizer, 11-circulating pump, 12-dosage bunker, 13-liquid-solid separator, 14-mother liquor storage tank, 15-fresh feed liquid, 16-cooler, 17-mother liquor concentrator, 18-flowmeter, 19-control valve, 20-thermostat, 21-agitator, 22-thermometer.
Detailed description of the invention
Below in conjunction with accompanying drawing, by embodiment to the structure of spiral-flow type fluidized-bed crystallizer described in the utility model and and the combination of miscellaneous equipment be described further.
Embodiment 1
In the present embodiment, the structure of spiral-flow type fluidized-bed crystallizer as shown in Figure 1, be made up of bed body, described bed body is the assembly of stainless steel cylinder 2 and stainless steel conic tube 1, the internal diameter of the large end of conic tube is identical with the internal diameter of cylinder, and the vertex of a cone of conic tube is arc-shaped, and conic tube 1 is positioned at the below of cylinder 2, its large end forms integral structure with the lower end of cylinder by welding, and should ensure the dead in line of cylinder 2 and conic tube 1 during welding, the upper end closed of cylinder 2, this Closed End is provided with crystal seed and adds entrance 6, conic tube 1 lower section sidewall is provided with the feed pipe 3 adding feed liquid, described feed pipe is two, be separated by 180 ° around conic tube sustained height and distribute, each feed pipe is all positioned at the horizontal tangent direction (see Fig. 3) of conic tube, added feed liquid is made to form eddy flow, the vertex of a cone of conic tube 1 lower end is provided with crystal outlet 5, the upper portion side wall of cylinder 2 is provided with the discharge nozzle 4 exporting mother liquor, described discharge nozzle is positioned at the horizontal tangent direction of cylinder and the outlet of discharge nozzle consistent with the eddy flow rotation direction that feed liquid is formed (see Fig. 2).
Structural parameters and the range of choice thereof of spiral-flow type fluidized-bed crystallizer described in the present embodiment are as follows:
1, the height L of conic tube
1=(0.5 ~ 1.2) D, the height L of cylinder
2=(1 ~ 5) D, the distance L between the vertex of a cone outer wall of feed pipe center line and conic tube
3=(0.3 ~ 0.5) L
1described D is the internal diameter of cylinder, the internal diameter D of cylinder mainly determines (such as according to the volume crystalline rate of crystallizing system and the production capacity of crystallizer, it is the cyclone fluidized bed crystallizer of potassium dihydrogen phosphate of 1t/h to production capacity, the internal diameter D of cylinder can be designed to 1.3m ~ 1.8m), for same crystallizing system, required production capacity is larger, the corresponding increase of internal diameter of cylinder.
2, the center line of crystal outlet and the angle α of bed body center line are 30 ° ~ 45 °.
Embodiment 2
In the present embodiment, the structure of spiral-flow type fluidized-bed crystallizer as shown in Figure 4, is made up of bed body and cooling jacket 9.Described bed body is the assembly of stainless steel cylinder 2 and stainless steel conic tube 1, the internal diameter of the large end of conic tube is identical with the internal diameter of cylinder, the vertex of a cone of conic tube is arc-shaped, conic tube 1 is positioned at the below of cylinder 2, its large end forms integral structure with the lower end of cylinder by welding, and should ensure the dead in line of cylinder 2 and conic tube 1 during welding, the upper end closed of cylinder 2, this Closed End is provided with crystal seed and adds entrance 6, conic tube 1 lower section sidewall is provided with the feed pipe 3 adding feed liquid, described feed pipe is four, be separated by 90 ° around conic tube sustained height and distribute, each feed pipe is all positioned at the horizontal tangent direction of conic tube, added feed liquid is made to form eddy flow, the vertex of a cone of conic tube 1 lower end is provided with crystal outlet 5, the upper portion side wall of cylinder 2 is provided with the discharge nozzle 4 exporting mother liquor, described discharge nozzle is positioned at the horizontal tangent direction of cylinder and the outlet of discharge nozzle is consistent with the eddy flow rotation direction that feed liquid is formed.Described cooling jacket 9 is arranged around the external wall of bed, there is cooling water inlet 7 its underpart, coolant outlet 8 is arranged at its top, cooling water inlet is arranged along the tangential direction of cooling jacket, cooling water rises in the shape of a spiral in chuck, coolant outlet is also arranged along the tangential direction of cooling jacket, and consistent with the eddy flow rotation direction that cooling water is formed.The eddy flow direction of cooling jacket inner cooling water is contrary with the eddy flow direction of feed liquid in crystallizer.
Structural parameters and the range of choice thereof of spiral-flow type fluidized-bed crystallizer described in the present embodiment are as follows:
1, the height L of conic tube
1=(0.5 ~ 1.2) D, the height L of cylinder
2=(1 ~ 5) D, the distance L between the vertex of a cone outer wall of feed pipe center line and conic tube
3=(0.3 ~ 0.5) L
1, described D is the internal diameter of cylinder.The internal diameter D of cylinder mainly determines according to the volume crystalline rate of crystallizing system and the production capacity of crystallizer, and for same crystallizing system, required production capacity is larger, the corresponding increase of internal diameter of cylinder.
2, the center line of crystal outlet and the angle α of bed body center line are 30 ° ~ 45 °.
Embodiment 3
Spiral-flow type fluidized-bed crystallizer in embodiment 2 and miscellaneous equipment are combined into a kind of periodic crystallisation system by the present embodiment, its structure is shown in Fig. 6, as can be seen from Figure 6, this periodic crystallisation system comprises spiral-flow type fluidized-bed crystallizer 10, circulating pump 11, dosage bunker 12, liquid-solid separator 13 and mother liquor storage tank 14.The discharge nozzle that the feed tube of circulating pump 11 is arranged by pipe fitting and the bed body forming spiral-flow type fluidized-bed crystallizer 10 is connected, the feed pipe that the drain pipe of circulating pump 11 is arranged by pipe fitting and the bed body forming spiral-flow type fluidized-bed crystallizer 10 is connected, dosage bunker 12 is placed on a high position, its discharging opening is connected with the pipe fitting being connected circulating pump 11 drain pipe by pipe fitting, the crystal that the charging aperture of liquid-solid separator 13 and the bed body of formation spiral-flow type fluidized-bed crystallizer 10 are arranged exports and connects, its liquid outlet connects with mother liquor storage tank 14, the crystal that mother liquor storage tank 14 is also arranged with bed body exports and is connected.
Described in the present embodiment, the operation of periodic crystallisation system is as follows:
1, fresh feed liquid 15 is transported to after the high-order dosage bunker 12 placed is prepared burden and reaches close to saturated degree, then the feed liquid in dosage bunker is sent in cyclone fluidized bed crystallizer 10, when the feed liquid liquid level in described crystallizer 10 bodies rises to more than the discharging opening of setting 8 ~ 12cm, stop reinforced;
2, ON cycle pump 11 makes the feed liquid in crystallizer 10 bodies be swirling two-phase flows state, in cooling jacket 9, pass into cooling water simultaneously, when in crystallizer 10 bodies, feed liquid is cooled to Metastable zone, the crystal seed arranged from bed body adds that entrance 6 is disposable adds quantitative crystal seed, crystal seed is dispersed and be suspended in the crystal region of a body in eddy flow feed liquid, carries out decrease temperature crystalline;
3, when liquidus temperature in crystallizer drops to higher than room temperature 5 ~ 10 DEG C, close circulating pump 11 and leave standstill 3 ~ 5min, so that crystal sedimentation, then the crystal outlet 5 that a body is arranged is opened, Crystal suspensions is discharged and is separated by liquid-solid separator 13, when contained crystal is little in suspension to be discharged, supernatant mother liquor is directly imported mother liquor storage tank 14;
4, the wet crystal of discharging from liquid-solid separator is carried out dry product, by the mother liquor feeding mother liquor storage tank 14 of discharging from liquid-solid separator, the mother liquor in mother liquor storage tank returns dosage bunker 12 after treatment, after preparing burden with fresh feed liquid, for the later crystallization cycle.
Embodiment 4
Spiral-flow type fluidized-bed crystallizer in embodiment 1 and miscellaneous equipment are combined into a kind of continuous crystallizing system by the present embodiment, its structure is shown in Fig. 7, as can be seen from Figure 7, this continuous crystallizing system comprises spiral-flow type fluidized-bed crystallizer 10, circulating pump 11, dosage bunker 12, liquid-solid separator 13, cooler 16 and mother liquor concentrator 17.The feed tube of circulating pump 11 is connected by the discharging opening of pipe fitting with dosage bunker 12, its drain pipe is connected by the inlet of pipe fitting with cooler 16, and the liquid outlet of cooler 16 is connected with the feed pipe that the bed body forming spiral-flow type fluidized-bed crystallizer 10 is arranged by pipe fitting; The discharge nozzle that the inlet of mother liquor concentrator 17 is arranged by pipe fitting and the bed body forming spiral-flow type fluidized-bed crystallizer 10 is connected, and its liquid outlet is connected by the inlet of pipe fitting with dosage bunker 12; The crystal that the charging aperture of liquid-solid separator 13 and the bed body of formation spiral-flow type fluidized-bed crystallizer 10 are arranged exports and connects, and its liquid outlet is connected by the inlet of pipe fitting with mother liquor concentrator 17.
The crystallization process of continuous crystallizing system described in the present embodiment under constant flow, temperature and degree of supersaturation continuously, carry out to stable state.The operating process of continuous crystalizer is as follows:
Feed liquid is sent into after cooler 16 cooling through circulating pump 11, the bed body entering spiral-flow type fluidized-bed crystallizer 10 carries out crystallization, the temperature of controlled cooling model device, the degree of supersaturation of feed liquid is made to be in Metastable zone, be as the criterion with unautogenous nucleation, meanwhile, the crystal seed arranged from bed body adds entrance 6 and adds crystal seed continuously, quantitatively; The crystal outlet 5 arranged from bed body after feed liquid completes crystallization process in the bed body of crystallizer 10 is discharged, and enters liquid-solid separator 13 and is separated; The wet crystal of discharging from liquid-solid separator carries out dry product, the mother liquor of discharging from liquid-solid separator is admitted to mother liquor concentrator 17, mother liquor after evaporation and concentration enters to be sent into cooler 16 through circulating pump 11 after dosage bunker 12 mixes with fresh feed liquid 15 and cools, then the bed body entering crystallizer 10 carries out crystallization; , so circulate, form continuous print crystallization process.
Embodiment 5
Spiral-flow type fluidized-bed crystallizer in embodiment 1 and miscellaneous equipment are combined into potassium dihydrogen phosphate crystal system by the present embodiment, its structure is shown in Fig. 8, as can be seen from Figure 8, this crystal system comprises spiral-flow type fluidized-bed crystallizer 10, circulating pump 11, cooler 16, flowmeter 18, thermostat 20 and agitator 21.The feed tube of circulating pump 11 is connected with thermostat 20 by pipe fitting, its drain pipe is connected by the inlet of pipe fitting with flowmeter 18, the inlet of cooler 16 is connected by the liquid outlet of pipe fitting with flowmeter 18, and the feed pipe that the liquid outlet of cooler 16 is arranged by pipe fitting and the bed body forming spiral-flow type fluidized-bed crystallizer 10 is connected; The discharge nozzle that thermostat 20 is arranged by pipe fitting and the bed body forming spiral-flow type fluidized-bed crystallizer 10 is connected, agitator 21 and protractor 22 is provided with in thermostat 20, the pipe fitting of connection thermostat 20 and circulating pump 11 is provided with control valve 19, and the bed body of spiral-flow type fluidized-bed crystallizer 10 is provided with thermometer.
In the present embodiment, the structural parameters of spiral-flow type fluidized-bed crystallizer 10 are as follows:
The internal diameter D=30mm of cylinder 2, the height L of conic tube 1
1the height L of=25mm cylinder 2
2=150mm, the distance L between the vertex of a cone outer wall of feed pipe 3 center line and conic tube
3=10mm, feed pipe 3 internal diameters=4mm, discharge nozzle 4 internal diameters=6mm, crystal seed adds the internal diameter=10mm of entrance 6, the internal diameter=5mm of crystal outlet 5, the crystal outlet center line of 5 and angle α=40 ° of bed body center line.
In the present embodiment, in thermostat 20, the temperature of feed liquid controls at 43 DEG C, and feed rate is 84.26Lh
-1, in spiral-flow type fluidized-bed crystallizer 10 bodies, potassium dihydrogen phosphate crystalline mother solution temperature is 40 DEG C, and mother liquor degree of supersaturation is 20gL
-1.The present embodiment operation is as follows: the feed liquid prepared is placed in thermostat 20, feed liquid enters cooler 16 and is cooled to supersaturated solution under the effect of circulating pump 11 after flowmeter 18 measures, supersaturated solution enters spiral-flow type fluidized-bed crystallizer 10 bodies through feed pipe, the discharge nozzle that mother liquor is arranged from spiral-flow type fluidized-bed crystallizer 10 body tops flows out, and enters thermostat 20; The crystal seed arranged from spiral-flow type fluidized-bed crystallizer 10 body tops after flow process is stablized adds entrance and adds crystal seed, after crystallization 0.5h, closes circulating pump 11, discharging, filtration, drying after leaving standstill 1min, sieves and weighs.Experimental result is in table 1:
Table 1
As can be seen from Table 1: the mass fraction that the mass fraction of the crystal grain of <0.9mm is only the crystal grain of 10.94%, >1.66mm is only 2.17%, the granularity of potassium dihydrogen phosphate crystal mainly at 0.9-1.66mm, narrow particle size distribution.
Comparative example
This comparative example adopts stirring-type crystallizer to carry out crystallization experiment to potassium dihydrogen phosphate.In the periodic crystallisation device of 250mL, prepare potassium dihydrogen phosphate with neutralisation, control rotating speed is 150r/min, and after solution reaches supersaturation, add seeded crystallization 2.5h, gained crystalline product size distribution is in table 2.
Table 2
Comparison sheet 1 and table 2 can be found out, spiral-flow type fluidized-bed crystallizer described in the utility model is compared with stirring-type crystallizer, and crystalline product size distribution is narrower, and crystal particle diameter increases.
The volume crystalline rate of contrast crystallizer, the volume crystalline rate of stirring-type crystallizer is 95.03kg/ (m
3h), the volume crystalline rate of spiral-flow type fluidized-bed crystallizer described in the utility model is 483.18kg/ (m
3h), be 5 times of stirring-type crystallizer.
Claims (9)
1. a spiral-flow type fluidized-bed crystallizer, comprise a body, it is characterized in that described bed body is the assembly of cylinder (2) and conic tube (1), the internal diameter of the large end of conic tube is identical with the internal diameter of cylinder, the vertex of a cone of conic tube is arc-shaped, conic tube (1) is positioned at the below of cylinder (2), and its large end is connected with the lower end of cylinder;
The upper end closed of cylinder (2), the end face of cylinder upper end is provided with crystal seed and adds entrance (6), conic tube (1) lower section sidewall is provided with the feed pipe (3) adding feed liquid, described feed pipe is at least two, be uniformly distributed around conic tube sustained height, each feed pipe is all positioned at the horizontal tangent direction of conic tube, added feed liquid is made to form eddy flow, the vertex of a cone of conic tube (1) lower end is provided with crystal outlet (5), the upper portion side wall of cylinder (2) is provided with the discharge nozzle (4) exporting mother liquor, described discharge nozzle is positioned at the horizontal tangent direction of cylinder and the outlet of discharge nozzle is consistent with the eddy flow rotation direction that feed liquid is formed.
2. spiral-flow type fluidized-bed crystallizer according to claim 1, is characterized in that the height L of conic tube (1)
1=(0.5 ~ 1.2) D, the height L of cylinder (2)
2=(1 ~ 5) D, described D is the internal diameter of cylinder.
3. spiral-flow type fluidized-bed crystallizer according to claim 1 or 2, is characterized in that the distance L between feed pipe (3) center line and the vertex of a cone outer wall of conic tube
3=(0.3 ~ 0.5) L
1, described L
1for the height of conic tube.
4. spiral-flow type fluidized-bed crystallizer according to claim 1 or 2, is characterized in that the crystal outlet center line of (5) and the angle (α) of bed body center line are 30 ° ~ 45 °.
5. spiral-flow type fluidized-bed crystallizer according to claim 3, is characterized in that the crystal outlet center line of (5) and the angle (α) of bed body center line are 30 ° ~ 45 °.
6. spiral-flow type fluidized-bed crystallizer according to claim 1 or 2, characterized by further comprising cooling jacket (9), described cooling jacket is arranged around the external wall of bed, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
7. spiral-flow type fluidized-bed crystallizer according to claim 3, characterized by further comprising cooling jacket (9), described cooling jacket is arranged around the external wall of bed, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
8. spiral-flow type fluidized-bed crystallizer according to claim 4, characterized by further comprising cooling jacket (9), described cooling jacket is arranged around the external wall of bed, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
9. spiral-flow type fluidized-bed crystallizer according to claim 5, characterized by further comprising cooling jacket (9), described cooling jacket is arranged around the external wall of bed, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
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| CN201420460547.5U CN204034311U (en) | 2014-08-15 | 2014-08-15 | A kind of spiral-flow type fluidized-bed crystallizer |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104162288A (en) * | 2014-08-15 | 2014-11-26 | 四川大学 | Rotational flow type fluidized bed crystallizer |
| CN107653483A (en) * | 2017-11-30 | 2018-02-02 | 河南恒星科技股份有限公司 | Exempt from stirring energy-conservation female groove |
| CN110204127A (en) * | 2019-07-09 | 2019-09-06 | 北京能为科技股份有限公司 | A kind of outside crystal seed method inhibits the system and its orientation scaling method of calcium salt scale |
-
2014
- 2014-08-15 CN CN201420460547.5U patent/CN204034311U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104162288A (en) * | 2014-08-15 | 2014-11-26 | 四川大学 | Rotational flow type fluidized bed crystallizer |
| CN104162288B (en) * | 2014-08-15 | 2016-06-29 | 四川大学 | A kind of spiral-flow type fluidized-bed crystallizer |
| CN107653483A (en) * | 2017-11-30 | 2018-02-02 | 河南恒星科技股份有限公司 | Exempt from stirring energy-conservation female groove |
| CN110204127A (en) * | 2019-07-09 | 2019-09-06 | 北京能为科技股份有限公司 | A kind of outside crystal seed method inhibits the system and its orientation scaling method of calcium salt scale |
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