CN104162288A - Rotational flow type fluidized bed crystallizer - Google Patents
Rotational flow type fluidized bed crystallizer Download PDFInfo
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- CN104162288A CN104162288A CN201410401028.6A CN201410401028A CN104162288A CN 104162288 A CN104162288 A CN 104162288A CN 201410401028 A CN201410401028 A CN 201410401028A CN 104162288 A CN104162288 A CN 104162288A
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Abstract
The invention discloses a rotational flow type fluidized bed crystallizer. The rotational flow type fluidized bed crystallizer comprises a bed body, wherein the bed body is formed by combining a cylinder and a cone cylinder; the inner diameter of the large end of the cone cylinder is equal to that of the cylinder; the cone top of the cone cylinder is of a circular arc shape; the cone cylinder is positioned below the cylinder; the large end of the cone cylinder is connected with the lower end of the cylinder; the upper end of the cylinder is closed; a seed crystal adding opening is formed in the end surface of the upper end of the cylinder; at least two feeding pipes for adding material liquid are arranged on the side wall of the lower section of the cone cylinder and are uniformly distributed around the cone cylinder at the same height; each feeding pipe is positioned in the horizontal tangential direction of the cone cylinder; a crystal outlet is formed in the cone top of the lower end of the cone cylinder; a discharging pipe for outputting mother liquid is arranged on the side wall of the upper part of the cylinder and is positioned in the horizontal tangential direction of the cylinder, and an outlet of the discharging pipe is in accordance with the rotational direction of rotational flow formed by the material liquid. In order to meet requirements of a clearance crystallization process, a cooling jacket can be arranged on the basis of the 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 operations in chemical products preparation, stirring tank crystallizer is the crystallizer generally using, because the stirrer paddle of this type of crystallizer has strong fragmentation to crystal, thereby secondary nucleation speed is high, crystalline product particle diameter is little, size distribution is wide, and crystal morphology is poor, is difficult to meet the requirement of some chemical products.
Theoretically, obtain epigranular, the neat crystalline product of crystalline form, it is crucial controlling secondary nucleation.For this reason, have researchers by fluidization technology for crystallization process, to avoid stirrer paddle to the broken of crystal and to reduce secondary nucleation speed.In the paper " sandy aluminium hydroxide crystallization experiment research in spouted fluidized bed " of delivering as people such as Zhao Kun, study spouted fluidized bed and (seen " Sichuan metallurgy " in the application of crystallization process, the 2nd phase of 33 volumes, 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 stronger, and the crystalline form of crystalline product and size distribution are still undesirable.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind of spiral-flow type fluidized-bed crystallizer is provided, 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, 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 circular-arc, 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, on the end face of cylinder upper end, be provided with crystal seed and add entrance, conic tube lower section sidewall is provided with the feed pipe that adds 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, make added feed liquid 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 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 forms.
In order better to realize goal of the invention, spiral-flow type fluidized-bed crystallizer of the present invention has been 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, the internal diameter that described D is cylinder, the inner diameter D of cylinder is mainly determined according to the production capacity of the volume crystalline rate of crystallizing system and crystallizer.
2, the distance L between the vertex of a cone outer wall of 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 is 30 °～45 ° with the angle α of bed body center line.
In order to meet the requirement of periodic crystallisation technique, can on the basis of said structure, cooling jacket be set, described cooling jacket is around the external wall setting 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 of the present invention: 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 upwards mobile (seeing Fig. 5), suspension crystal circles under the effect of eddy flow feed liquid, and continuous crystal growth, to grow up to suspending power can not balance self gravitation time when crystal, the bottom of falling voluntarily crystallizer 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, is turned back to the feed pipe of crystallizer by circulating pump, realizes the circulation of feed liquid.
The present invention has following beneficial effect:
1, because forming slow screw type rotary upwards in the bed body of crystallizer of the present invention, feed liquid flows, suspension crystal circles around bed body axis, and in crystal growth process, there is no the strong impaction of stirrer paddle, thereby uniform crystal dispersion crystal growth in feed liquid, can be not chipping, the speed of secondary nucleation greatly weakens, and the grain number of gained crystal product approaches with the grain number that drops into crystal seed, narrow particle size distribution, pattern neat (seeing embodiment).
2, crystallizer of the present invention and miscellaneous equipment combination, can meet the requirement of periodic crystallisation and continuous crystallisation technique.
3, the bed body of crystallizer of the present invention is interior without any member, thereby is difficult for blockage phenomenon, stable work in work.
4, mold structure of the present invention is simple, is easy to processing and fabricating, thereby investment cost is few, is conducive to promote the use of.
Brief description of the drawings
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 and miscellaneous equipment are combined into;
Fig. 7 is a kind of continuous crystallizing system that spiral-flow type fluidized-bed crystallizer of the present invention and miscellaneous equipment are combined into;
Fig. 8 is the experimental provision system diagram of spiral-flow type fluidized-bed crystallizer of the present invention for potassium dihydrogen phosphate crystallization;
Fig. 9 is the optical photograph that uses the prepared potassium dihydrogen phosphate crystal of experimental provision system described in Fig. 8;
Figure 10 is the enlarged drawing that uses the prepared potassium dihydrogen phosphate crystal of experimental provision system described in Fig. 8.
In figure, 1-conic tube, 2-cylinder, the feed pipe of 3-feed liquid, the discharge nozzle of 4-output mother liquor, the outlet of 5-crystal, 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 inspissator, 18-flowmeter, 19-control valve, 20-thermostat, 21-agitator, 22-thermometer.
Detailed description of the invention
Below in conjunction with accompanying drawing, the structure by embodiment to spiral-flow type fluidized-bed crystallizer of the present invention and being described further with the combination of miscellaneous equipment.
Embodiment 1
In the present embodiment, the structure of spiral-flow type fluidized-bed crystallizer as shown in Figure 1, formed by 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 circular-arc, and conic tube 1 is positioned at the below of cylinder 2, the lower end of its large end and cylinder forms integral structure by welding, should ensure the dead in line of cylinder 2 and conic tube 1 when welding, the upper end closed of cylinder 2, on this Closed End, be provided with crystal seed and add entrance 6, conic tube 1 lower section sidewall is provided with the feed pipe 3 that adds feed liquid, described feed pipe is two, around the 180 ° of distributions of being separated by of conic tube sustained height, each feed pipe is all positioned at the horizontal tangent direction (seeing Fig. 3) of conic tube, make added feed liquid 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 liquor, described discharge nozzle is positioned at the eddy flow rotation direction consistent (seeing Fig. 2) that the horizontal tangent direction of cylinder and the outlet of discharge nozzle form with feed liquid.
Described in the present embodiment, the structural parameters of spiral-flow type fluidized-bed crystallizer and range of choice thereof 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 inner diameter D of cylinder mainly (for example determines according to the production capacity of the volume crystalline rate of crystallizing system and crystallizer, the cyclone fluidized bed crystallizer of potassium dihydrogen phosphate that is 1t/h to production capacity, the inner 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 is 30 °～45 ° with the angle α of bed body center line.
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 circular-arc, conic tube 1 is positioned at the below of cylinder 2, the lower end of its large end and cylinder forms integral structure by welding, should ensure the dead in line of cylinder 2 and conic tube 1 when welding, the upper end closed of cylinder 2, on this Closed End, be provided with crystal seed and add entrance 6, conic tube 1 lower section sidewall is provided with the feed pipe 3 that adds feed liquid, described feed pipe is four, around the 90 ° of distributions of being separated by of conic tube sustained height, each feed pipe is all positioned at the horizontal tangent direction of conic tube, make added feed liquid 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 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 forms.Described cooling jacket 9 is around the external wall setting of bed, there is cooling water inlet 7 its underpart, coolant outlet 8 is arranged at its top, cooling water inlet is along the tangential direction setting of cooling jacket, cooling water rises in the shape of a spiral in chuck, coolant outlet is also along the tangential direction setting of cooling jacket, and the eddy flow rotation direction forming with cooling water is consistent.The eddy flow opposite direction of feed liquid in the eddy flow direction of cooling water and crystallizer in cooling jacket.
Described in the present embodiment, the structural parameters of spiral-flow type fluidized-bed crystallizer and range of choice thereof 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, the internal diameter that described D is cylinder.The inner diameter D of cylinder is mainly according to the production capacity decision of the volume crystalline rate of crystallizing system and 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 is 30 °～45 ° with the angle α of bed body center line.
Embodiment 3
The 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 feed tube of circulating pump 11 is connected with the discharge nozzle that the bed body that forms spiral-flow type fluidized-bed crystallizer 10 arranges by pipe fitting, the drain pipe of circulating pump 11 is connected with the feed pipe that the bed body that forms spiral-flow type fluidized-bed crystallizer 10 arranges by pipe fitting, dosage bunker 12 is placed on a high position, its discharging opening connects with the pipe fitting that is connected circulating pump 11 drain pipes by pipe fitting, the charging aperture of liquid-solid separator 13 joins with the crystal outlet of the bed body setting that forms spiral-flow type fluidized-bed crystallizer 10, its liquid outlet and mother liquor storage tank 14 join, the crystal outlet that mother liquor storage tank 14 also arranges 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 the saturated degree that approaches after being transported to the high-order dosage bunker of placing 12 batchings, then the feed liquid in dosage bunker is sent in cyclone fluidized bed crystallizer 10, more than rising to the discharging opening of setting, the feed liquid liquid level in 10 bodies of described crystallizer when 8～12cm, stops feeding in raw material;
2, ON cycle pump 11 makes the feed liquid in 10 bodies of crystallizer be eddy flow flow regime, in cooling jacket 9, pass into cooling water simultaneously, in the time that in 10 bodies of crystallizer, feed liquid is cooled to Jie Wen district, add from the crystal seed of bed body setting 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, in the time that liquidus temperature in crystallizer drops to higher than 5～10 DEG C of room temperatures, close circulating pump 11 and leave standstill 3～5min, so that crystal sedimentation, then open the crystal outlet 5 that a body arranges, crystal suspension is discharged and separated by liquid-solid separator 13, when contained crystal is little in the suspension of discharging, supernatant mother liquor is directly imported to mother liquor storage tank 14;
4, the wet crystal of discharging from liquid-solid separator is dried to obtain to product, the mother liquor of discharging from liquid-solid separator is sent into mother liquor storage tank 14, the mother liquor in mother liquor storage tank returns to dosage bunker 12 after treatment, after fresh feed liquid batching, for follow-up crystallizing cycle.
Embodiment 4
The 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 inspissator 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 arranging with the bed body that forms spiral-flow type fluidized-bed crystallizer 10 by pipe fitting; The inlet of mother liquor inspissator 17 is connected with the discharge nozzle that the bed body that forms spiral-flow type fluidized-bed crystallizer 10 arranges by pipe fitting, and its liquid outlet is connected with the inlet of dosage bunker 12 by pipe fitting; The charging aperture of liquid-solid separator 13 joins with the crystal outlet of the bed body setting that forms spiral-flow type fluidized-bed crystallizer 10, and its liquid outlet is connected with the inlet of mother liquor inspissator 17 by pipe fitting.
Described in the present embodiment the crystallization process of continuous crystallizing system 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 through circulating pump 11 send into cooler 16 cooling after, the bed body that enters spiral-flow type fluidized-bed crystallizer 10 carries out crystallization, control the temperature of cooler, make the degree of supersaturation of feed liquid in Jie Wen district, be as the criterion with unautogenous nucleation, meanwhile, add entrance 6 from the crystal seed of bed body setting and continuously, quantitatively add crystal seed; The crystal outlet 5 that feed liquid arranges from bed body complete crystallization process in the bed body of crystallizer 10 after is discharged, and enters liquid-solid separator 13 and separates; The wet crystal of discharging from liquid-solid separator is dried to obtain product, the mother liquor of discharging from liquid-solid separator is admitted to mother liquor inspissator 17, mother liquor after evaporation and concentration enters that after dosage bunker 12 mixes with fresh feed liquid 15, to send into cooler 16 through circulating pump 11 cooling, then a bed body that enters crystallizer 10 carries out crystallization; , so circulation, forms continuous crystallization process.
Embodiment 5
The 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 with the inlet of flowmeter 18 by pipe fitting, the inlet of cooler 16 is connected with the liquid outlet of flowmeter 18 by pipe fitting, and the liquid outlet of cooler 16 is connected with the feed pipe that the bed body that forms spiral-flow type fluidized-bed crystallizer 10 arranges by pipe fitting; Thermostat 20 is connected with the discharge nozzle that the bed body that forms spiral-flow type fluidized-bed crystallizer 10 arranges by pipe fitting, in thermostat 20, be provided with agitator 21 and protractor 22, on the pipe fitting of connection thermostat 20 and circulating pump 11, be provided with control valve 19, a bed body for 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:
Inner diameter D=the 30mm of cylinder 2, the height L of conic tube 1
1the height L of=25mm cylinder 2
2=150mm, the distance L between feed pipe 3 center lines and the vertex of a cone outer wall of 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 center line of crystal outlet 5 and angle α=40 ° for body center line.
In the present embodiment, the temperature of thermostat 20 interior feed liquids is controlled at 43 DEG C, and feed rate is 84.26Lh
-1, in 10 bodies of spiral-flow type fluidized-bed crystallizer, potassium dihydrogen phosphate crystalline mother solution temperature is 40 DEG C, mother liquor degree of supersaturation is 20gL
-1.The present embodiment operation is as follows: the feed liquid preparing is placed in to thermostat 20, feed liquid enters cooler 16 and is cooled to supersaturated solution under the effect of circulating pump 11 after flowmeter 18 meterings, supersaturated solution enters 10 bodies of spiral-flow type fluidized-bed crystallizer through feed pipe, the discharge nozzle that mother liquor arranges from 10 body tops of spiral-flow type fluidized-bed crystallizer flows out, and enters thermostat 20; The crystal seed arranging from 10 body tops of spiral-flow type fluidized-bed crystallizer after flow process is stable adds entrance and adds crystal seed, after crystallization 0.5h, closes circulating pump 11, leaves standstill discharging, filtration after 1min, is dried, sieves and weigh.Experimental result is in table 1 and Fig. 9, Figure 10:
Table 1
Can find out from table 1 and Fig. 9, Figure 10:
(1) the potassium dihydrogen phosphate crystal size uniform (seeing Fig. 9) obtaining, crystalline form rule neat (seeing Figure 10).
(2) mass fraction of the crystal grain of <0.9mm is only 10.94%, the mass fraction of the crystal grain of >1.66mm is only 2.17%, the granularity of potassium dihydrogen phosphate crystal is mainly at 0.9-1.66mm, narrow particle size distribution (in table 1).
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, when solution reaches after supersaturation, adds seeded crystallization 2.5h, gained crystalline product size distribution is in table 2.
Table 2
Comparison sheet 1 and table 2 can find out, spiral-flow type fluidized-bed crystallizer of the present invention 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 of the present invention 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 circular-arc, 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), on the end face of cylinder upper end, be provided with crystal seed and add entrance (6), conic tube (1) lower section sidewall is provided with the feed pipe (3) that adds 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, make added feed liquid 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 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 forms.
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, the internal diameter that described D is cylinder.
3. according to spiral-flow type fluidized-bed crystallizer described in claim 1 or 2, it 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. according to spiral-flow type fluidized-bed crystallizer described in claim 1 or 2, it is characterized in that the center line of crystal outlet (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 center line of crystal outlet (5) and an angle (α) for bed body center line are 30 °～45 °.
6. according to spiral-flow type fluidized-bed crystallizer described in claim 1 or 2, characterized by further comprising cooling jacket (9), described cooling jacket is around the external wall setting 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 around the external wall setting 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 around the external wall setting 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 around the external wall setting of bed, and there is cooling water inlet (7) its underpart, and coolant outlet (8) is arranged at its top.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106636682A (en) * | 2016-12-22 | 2017-05-10 | 神华集团有限责任公司 | Equipment and method for preparing high purity gallium |
| 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 |
| JP2019202283A (en) * | 2018-05-24 | 2019-11-28 | 水ｉｎｇ株式会社 | Processing method of liquid to be treated of and processing apparatus of liquid to be treated |
| CN113599858A (en) * | 2021-08-11 | 2021-11-05 | 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 |
| JP2022008913A (en) * | 2018-05-24 | 2022-01-14 | 水ｉｎｇ株式会社 | Processing method of liquid to be treated of and processing apparatus of liquid to be treated |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005246199A (en) * | 2004-03-03 | 2005-09-15 | Tokyo Metropolis | Chemical pouring nozzle for crystallization tank |
| 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 |
-
2014
- 2014-08-15 CN CN201410401028.6A patent/CN104162288B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005246199A (en) * | 2004-03-03 | 2005-09-15 | Tokyo Metropolis | Chemical pouring nozzle for crystallization tank |
| 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 |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN106636682A (en) * | 2016-12-22 | 2017-05-10 | 神华集团有限责任公司 | Equipment and method for preparing high purity gallium |
| JP7206061B2 (en) | 2018-05-24 | 2023-01-17 | 水ｉｎｇ株式会社 | Method for treating liquid to be treated |
| JP2019202283A (en) * | 2018-05-24 | 2019-11-28 | 水ｉｎｇ株式会社 | Processing method of liquid to be treated of and processing apparatus of liquid to be treated |
| JP2022008913A (en) * | 2018-05-24 | 2022-01-14 | 水ｉｎｇ株式会社 | Processing method of liquid to be treated of and processing apparatus of liquid to be treated |
| 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 |
| 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 |
| CN113599858A (en) * | 2021-08-11 | 2021-11-05 | 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 |
| 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 |
| CN114849270A (en) * | 2022-05-31 | 2022-08-05 | 中国石油化工股份有限公司 | Sulphur granule shaping pre crystallization device |
| 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 |
| CN116550118A (en) * | 2023-07-09 | 2023-08-08 | 浙江百能科技有限公司 | Integrated separation device and method for activating absorption crystallization |
| 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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