CN104162288B - 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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- CN104162288B CN104162288B CN201410401028.6A CN201410401028A CN104162288B CN 104162288 B CN104162288 B CN 104162288B CN 201410401028 A CN201410401028 A CN 201410401028A CN 104162288 B CN104162288 B CN 104162288B
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Abstract
A kind of spiral-flow type fluidized-bed crystallizer, including bed body, described bed body is the assembly of cylinder and conic tube, the internal diameter of the big 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 lower section of cylinder, and its big 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 at least two, it is uniformly distributed around conic tube sustained height, each feed pipe is respectively positioned on 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 of output mother solution, 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
Patent of the present invention belongs to the crystallization technique field of Chemical Engineering, relates to a kind of crystallizer.
Background technology
Crystallization is a unit operation in chemical products preparation, stirring tank crystallizer is the crystallizer commonly used, owing to crystal is had strong fragmentation by the stirrer paddle of this type of crystallizer, thus secondary nucleation speed is high, crystalline product particle diameter is little, particle size distribution width, crystal morphology is poor, it is difficult to meet the requirement of some chemical products.
Theoretically, will obtaining the crystalline product that epigranular, crystal form are neat, it is crucial for controlling secondary nucleation.For this, have researcheres that fluidization technology is used for crystallization process, to avoid stirrer paddle to the broken of crystal and to reduce secondary nucleation speed.The spouted fluidized bed application at crystallization process is have studied (see " Sichuan is metallurgical " in Zhao Kun et al. paper " in spouted fluidized bed the research of sandy aluminium hydroxide crystallization experiment " delivered, 33 volume the 2nd phases, 63～66 pages), but this crystallization fluid bed is confined to tradition fluidization process, the internal turbulence of bed is violent, secondary nucleation is still relatively strong, and the crystal form of crystalline product and particle size distribution are still undesirable.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art, it is provided that a kind of spiral-flow type fluidized-bed crystallizer, to reduce the secondary nucleation speed in crystallization process, increase the particle diameter of crystalline product, and make crystalline product narrow particle size distribution, pattern neat.
Spiral-flow type fluidized-bed crystallizer of the present invention, including bed body, described bed body is the assembly of cylinder and conic tube, the internal diameter of the big 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 lower section of cylinder, and its big 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 at least two, it is uniformly distributed around conic tube sustained height, each feed pipe is respectively positioned on the horizontal tangent direction of conic tube, affiliated 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 of output mother solution, 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 of the present invention have selected following structural parameters:
1, the height L of conic tube1=(0.5～1.2) D, the height L of cylinder2D, described D are the internal diameter of cylinder in=(1～5), and the internal diameter D of cylinder mainly determines according to the volume crystalline rate of crystallizing system and the production capacity of crystallizer.
2, the distance L between the vertex of a cone outer wall of feed liquid feed pipe centrage and conic tube3=(0.3～0.5) L1, described L1Height for conic tube.
3, the centrage of crystal outlet is 30 °～45 ° with the angle α of bed body centrage.
In order to meet the requirement of batch crystallization process, can arranging cooling jacket on the basis of said structure, described cooling jacket is arranged around bed body outer wall, 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 of the present invention: crystal seed adds from crystallizer top, feed liquid tangentially enters from the tapered sidewalls of crystallizer bottom, mother solution is tangentially discharged from top cylinder sidewall, form screw type rotary flowing (see Fig. 5) slowly upwards, suspended crystal circles under the effect of eddy flow feed liquid, and continuous crystal growth, when crystal is grown up and can not be balanced self gravitation to suspending power, the bottom falling crystallizer voluntarily draws off from crystal outlet；The mother solution discharged from crystallizer top, supplements and heat exchange through fresh feed liquid, reaches required degree of supersaturation, circulating pump return to the feed pipe of crystallizer, it is achieved the circulation of feed liquid.
The method have the advantages that
1, owing to feed liquid forms slow screw type rotary flowing upwards in the bed body of crystallizer of the present invention, 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, will not be chipping, the speed of secondary nucleation greatly weakens, and the grain number of gained crystal product is close with the grain number putting into crystal seed, narrow particle size distribution, pattern neat (see embodiment).
2, crystallizer of the present invention and miscellaneous equipment combination, can meet periodic crystallisation and the requirement of continuous crystallisation technique.
3, without any component in the bed body of crystallizer of the present invention, thus it is not susceptible to clogging, stable work in work.
4, mold structure of the present invention is simple, it is 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 of the present invention；
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 of the present invention, is provided with cooling jacket；
Fig. 5 is the fundamental diagram of spiral-flow type fluidized-bed crystallizer of the present invention；
Fig. 6 is a kind of periodic crystallisation system that spiral-flow type fluidized-bed crystallizer of the present invention is combined into miscellaneous equipment；
Fig. 7 is a kind of continuous crystallizing system that spiral-flow type fluidized-bed crystallizer of the present invention is combined into miscellaneous equipment；
Fig. 8 is the spiral-flow type fluidized-bed crystallizer of the present invention experimental provision system diagram for potassium dihydrogen phosphate crystallization；
Fig. 9 is the optical photograph of the potassium dihydrogen phosphate crystal described in use Fig. 8 prepared by experimental provision system；
Figure 10 is the enlarged drawing of the potassium dihydrogen phosphate crystal described in use Fig. 8 prepared by experimental provision system.
In figure, 1 conic tube, 2 cylinders, the feed pipe of 3 feed liquids, the discharge nozzle of 4 output mother solutions, 5 crystal outlets, 6 crystal seeds add entrance, 7 cooling water inlets, 8 coolant outlets, 9 cooling jackets, 10 spiral-flow type fluidized-bed crystallizers, 11 circulating pumps, 12 dosage bunkers, 13 liquid-solid separators, 14 mother solution storage tanks, 15 fresh feed liquids, 16 coolers, 17 mother liquor concentrator, 18 effusion meters, 19 control valve, 20 temperature chambers, 21 agitators, 22 thermometeies.
Detailed description of the invention
Below in conjunction with accompanying drawing, the compound mode by the embodiment structure to spiral-flow type fluidized-bed crystallizer of the present invention and with miscellaneous equipment is described further.
Embodiment 1
In the present embodiment, the structure of spiral-flow type fluidized-bed crystallizer is as shown in Figure 1, it is made up of bed body, described bed body is rustless steel cylinder 2 and the assembly of rustless steel conic tube 1, the internal diameter of the big 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 lower section of cylinder 2, its big end forms integral structure with the lower end of cylinder by welding, and should ensure that cylinder 2 and the dead in line of 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, it is separated by 180 ° around conic tube sustained height and is distributed, each feed pipe is respectively positioned on the horizontal tangent direction (see Fig. 3) of conic tube, affiliated 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 of output mother solution, 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 tube1=(0.5～1.2) D, the height L of cylinder2=(1～5) D, the distance L between the vertex of a cone outer wall of feed pipe centrage and conic tube3=(0.3～0.5) L1Described D is the internal diameter of cylinder, the internal diameter D of cylinder mainly determines (such as according to the production capacity of the volume crystalline rate of crystallizing system and crystallizer, to the cyclone fluidized bed crystallizer of the potassium dihydrogen phosphate that production capacity is 1t/h, the internal diameter D of cylinder may be designed as 1.3m～1.8m), for same crystallizing system, required production capacity is more big, and the internal diameter of cylinder increases accordingly.
2, the centrage of crystal outlet is 30 °～45 ° with the angle α of bed body centrage.
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 rustless steel cylinder 2 and the assembly of rustless steel conic tube 1, the internal diameter of the big 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 lower section of cylinder 2, its big end forms integral structure with the lower end of cylinder by welding, and should ensure that cylinder 2 and the dead in line of 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, it is separated by 90 ° around conic tube sustained height and is distributed, each feed pipe is respectively positioned on the horizontal tangent direction of conic tube, affiliated 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 of output mother solution, 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 bed body outer wall, 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 in opposite direction with the eddy flow 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 tube1=(0.5～1.2) D, the height L of cylinder2=(1～5) D, the distance L between the vertex of a cone outer wall of feed pipe centrage and conic tube3=(0.3～0.5) L1, described D is the internal diameter of cylinder.The internal diameter D of cylinder mainly determines according to the production capacity of the volume crystalline rate of crystallizing system and crystallizer, and for same crystallizing system, required production capacity is more big, and the internal diameter of cylinder increases accordingly.
2, the centrage of crystal outlet is 30 °～45 ° with the angle α of bed body centrage.
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, from fig. 6, it can be seen that this periodic crystallisation system includes spiral-flow type fluidized-bed crystallizer 10, circulating pump 11, dosage bunker 12, liquid-solid separator 13 and mother solution storage tank 14.The discharge nozzle that the feed tube of circulating pump 11 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting is connected, the feed pipe that the drain pipe of circulating pump 11 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting 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 outlet that the charging aperture of liquid-solid separator 13 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 connects, its liquid outlet connects with mother solution storage tank 14, the crystal outlet that mother solution storage tank 14 is also arranged with bed body is connected.
Described in the present embodiment, the operation of periodic crystallisation system is as follows:
1, fresh feed liquid 15 reaches close to saturated degree after being transported to high-order dosage bunker 12 dispensing placed, 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 bed body 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 bed body be eddy flow flow regime, in cooling jacket 9, pass into cooling water simultaneously, when in crystallizer 10 bed body, feed liquid is cooled to Metastable zone, the crystal seed arranged from bed body adds the crystal seed that the disposable addition of entrance 6 is quantitative, crystal seed is dispersed and be suspended in the crystal region of bed body in eddy flow feed liquid, carries out decrease temperature crystalline；
3, when in crystallizer, liquidus temperature drops to higher than room temperature 5～10 DEG C, close circulating pump 11 and stand 3～5min, so that crystal settles, then the crystal outlet 5 that bed body is arranged is opened, Crystal suspensions is discharged and is easily separated by liquid-solid separator 13, when contained crystal is little in suspension to be discharged, supernatant mother solution is introduced directly into mother solution storage tank 14；
4, the wet crystal discharged from liquid-solid separator being dried to obtain product, the mother solution discharged from liquid-solid separator is sent into mother solution storage tank 14, the mother solution in mother solution storage tank returns dosage bunker 12 after treatment, after fresh feed liquid dispensing, 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, from figure 7 it can be seen that this continuous crystallizing system includes 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 with the discharging opening of dosage bunker 12 by pipe fitting, its drain pipe is connected with the inlet of cooler 16 by pipe fitting, and the liquid outlet of cooler 16 is connected with the feed pipe arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting；The discharge nozzle that the inlet of mother liquor concentrator 17 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting is connected, and its liquid outlet is connected with the inlet of dosage bunker 12 by pipe fitting；The crystal outlet that the charging aperture of liquid-solid separator 13 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 connects, and its liquid outlet is connected with the inlet of mother liquor concentrator 17 by pipe fitting.
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, control the temperature of cooler, the degree of supersaturation making feed liquid is in Metastable zone, it is as the criterion with unautogenous nucleation, meanwhile, the crystal seed arranged from bed body add entrance 6 continuously, be quantitatively adding crystal seed；Crystal outlet 5 discharge that feed liquid is arranged from bed body after completing crystallization process in the bed body of crystallizer 10, enters liquid-solid separator 13 and is easily separated；The wet crystal discharged from liquid-solid separator is dried to obtain product, the mother solution discharged from liquid-solid separator is admitted to mother liquor concentrator 17, mother solution entrance dosage bunker 12 after evaporation and concentration is sent into cooler 16 through circulating pump 11 after mixing with fresh feed liquid 15 and is cooled down, and the bed body entering back into 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, from figure 8, it is seen that this crystal system includes spiral-flow type fluidized-bed crystallizer 10, circulating pump 11, cooler 16, effusion meter 18, temperature chamber 20 and agitator 21.The feed tube of circulating pump 11 is connected with temperature chamber 20 by pipe fitting, its drain pipe is connected with the inlet of effusion meter 18 by pipe fitting, the inlet of cooler 16 is connected with the liquid outlet of effusion meter 18 by pipe fitting, and the feed pipe that the liquid outlet of cooler 16 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting is connected；The discharge nozzle that temperature chamber 20 is arranged with the bed body constituting spiral-flow type fluidized-bed crystallizer 10 by pipe fitting is connected, agitator 21 and protractor 22 it is provided with in temperature chamber 20, connecting and be provided with control valve 19 on the pipe fitting of temperature chamber 20 and circulating pump 11, 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 11The height L of=25mm cylinder 22=150mm, the distance L between the vertex of a cone outer wall of feed pipe 3 centrage and conic tube3=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, and crystal exports the centrage of 5 and angle α=40 ° of bed body centrage.
In the present embodiment, in temperature chamber 20, the temperature of feed liquid controls at 43 DEG C, and feed rate is 84.26L h-1, in spiral-flow type fluidized-bed crystallizer 10 bed body, potassium dihydrogen phosphate crystalline mother solution temperature is 40 DEG C, and mother solution degree of supersaturation is 20g L-1.The present embodiment operation is as follows: be placed in temperature chamber 20 by the feed liquid prepared, feed liquid enters cooler 16 cooling for supersaturated solution under the effect of circulating pump 11 after effusion meter 18 measures, supersaturated solution enters spiral-flow type fluidized-bed crystallizer 10 bed body through feed pipe, the discharge nozzle that mother solution is arranged from spiral-flow type fluidized-bed crystallizer 10 bed body top flows out, and enters temperature chamber 20；The crystal seed arranged from spiral-flow type fluidized-bed crystallizer 10 bed body top after flow process is stable adds entrance and adds crystal seed, after crystallization 0.5h, closes circulating pump 11, discharging, filtration after standing 1min, dries, sieves and weighs.Experimental result is in Table 1 and Fig. 9, Figure 10:
Table 1
From table 1 and Fig. 9, Figure 10 it can be seen that
(1) obtained potassium dihydrogen phosphate crystal size uniform (see Fig. 9), crystal form rule neat (see Figure 10).
(2) mass fraction of the crystal grain of<mass fraction of the crystal grain of 0.9mm is only 10.94%,>1.66mm is only 2.17%, and the granularity of potassium dihydrogen phosphate crystal is mainly at 0.9-1.66mm, narrow particle size distribution (see table 1).
Comparative example
This comparative example adopts stirring-type crystallizer that potassium dihydrogen phosphate is carried out crystallization experiment.In the periodic crystallisation device of 250mL, preparing potassium dihydrogen phosphate with neutralisation, control rotating speed is 150r/min, after solution reaches supersaturation, adds seeded crystallization 2.5h, and gained crystalline product particle size distribution is in Table 2.
Table 2
Comparison sheet 1 is with table 2 it can be seen that spiral-flow type fluidized-bed crystallizer of the present invention is compared with stirring-type crystallizer, and crystalline product particle 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/ (m3H), the volume crystalline rate of spiral-flow type fluidized-bed crystallizer of the present invention is 483.18kg/ (m3H), 5 times of formula crystallizer it are stirring for.
Claims (3)
1. a spiral-flow type fluidized-bed crystallizer, including bed body, it is characterised in that described bed body is cylinder (2) and the assembly of conic tube (1), 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, and the internal diameter of the big end of conic tube is identical with the internal diameter of cylinder, and the vertex of a cone of conic tube is arc-shaped, conic tube (1) is positioned at the lower section of cylinder (2), and its big 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 at least two, it is uniformly distributed around conic tube sustained height, each feed pipe is respectively positioned on the horizontal tangent direction of conic tube, affiliated feed liquid is made to form eddy flow, the distance L between each feed pipe (3) centrage and the vertex of a cone outer wall of conic tube3=(0.3～0.5) L1The 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) of output mother solution, 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.
2. spiral-flow type fluidized-bed crystallizer according to claim 1, it is characterised in that the centrage of crystal outlet (5) is 30 °～45 ° with the angle (α) of bed body centrage.
3. spiral-flow type fluidized-bed crystallizer according to claim 1 or claim 2, characterized by further comprising cooling jacket (9), described cooling jacket is arranged around bed body outer wall, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
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| CN106636682B (en) * | 2016-12-22 | 2019-04-02 | 神华集团有限责任公司 | A kind of device and method preparing high purity gallium |
| JP7301105B2 (en) * | 2018-05-24 | 2023-06-30 | 水ｉｎｇ株式会社 | Method for treating liquid to be treated and apparatus for treating liquid to be treated |
| JP7206061B2 (en) * | 2018-05-24 | 2023-01-17 | 水ｉｎｇ株式会社 | Method for treating liquid to be treated |
| CN109011667A (en) * | 2018-07-02 | 2018-12-18 | 四川大学 | Siphon vacuum rotational flow evaporating method and apparatus |
| CN110203955A (en) * | 2019-03-20 | 2019-09-06 | 昆明冶金研究院 | A kind of method that fluidized bed crystallisation removes organic matter in Alumina Produce Liquor |
| CN113599858B (en) * | 2021-08-11 | 2022-06-10 | 自然资源部天津海水淡化与综合利用研究所 | Spiral-flow type fluidized bed cooling crystallization system |
| CN114849270B (en) * | 2022-05-31 | 2024-05-14 | 中国石油化工股份有限公司 | Sulfur granule shaping crystallization device in advance |
| CN116550118B (en) * | 2023-07-09 | 2023-09-22 | 浙江百能科技有限公司 | Integrated separation device and method for activating absorption crystallization |
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| CN202506164U (en) * | 2012-04-20 | 2012-10-31 | 瓮福（集团）有限责任公司 | Large particle crystallizing equipment |
| CN204034311U (en) * | 2014-08-15 | 2014-12-24 | 四川大学 | A kind of spiral-flow type fluidized-bed crystallizer |
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| JP4308041B2 (en) * | 2004-03-03 | 2009-08-05 | 東京都 | Crystallization tank |
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| CN201092537Y (en) * | 2007-06-11 | 2008-07-30 | 娄爱娟 | Device for producing ammonium sulfate by smoke-gas ammonia process desulfuration |
| CN202506164U (en) * | 2012-04-20 | 2012-10-31 | 瓮福（集团）有限责任公司 | Large particle crystallizing equipment |
| CN204034311U (en) * | 2014-08-15 | 2014-12-24 | 四川大学 | A kind of spiral-flow type fluidized-bed crystallizer |
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