CN1792406A - Equipment for preparing high pure organic matter by fusion-crystallization method - Google Patents
Equipment for preparing high pure organic matter by fusion-crystallization method Download PDFInfo
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- CN1792406A CN1792406A CN 200510022137 CN200510022137A CN1792406A CN 1792406 A CN1792406 A CN 1792406A CN 200510022137 CN200510022137 CN 200510022137 CN 200510022137 A CN200510022137 A CN 200510022137A CN 1792406 A CN1792406 A CN 1792406A
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Abstract
A device for preparing high-purity organic substance by fusion crystallizing method is a tower structure which is divided into upper cooling-crystallizing segment, middle separating-purifying segment and lower crystal fusing segment. Its tower body is inclined and is composed of casing consisting of intersected two cylinders, heater and parallel engaged two spiral stirrers.
Description
Technical field
The invention belongs to the device of preparation high pure organic matter, particularly a kind of device that adopts preparing high pure organic matter by fusion-crystallization method.
Background technology
In recent years, the fast development along with industries such as medical industry, food industry, fine chemistry industry, macromolecular material engineerings increases day by day to the organic demand of high-purity in the world, and especially as the optically active body of pharmaceuticals, its purity requirement is high.The fusion-crystallization method has obtained using widely in industrial production as a kind of isolation and purification method of high-efficiency low energy consumption.
Operate by---washing---recrystallization owing to can finish crystallization simultaneously for tower crystallizer, it is the at present industrial fusion-crystallization method of generally the using organic device of purifying, but the tower crystallizer of which kind of structure no matter, purification mechanism includes countercurrent washing, recrystallization and sweating, and (crystal is when the temperature of a little higher than primary crystallization, the constantly fusing and the phenomenon of oozing out is sweating of its inner low melting point impurity, sweating is further purified crystal).In the above-mentioned mechanism, the sweating process is to determine whether to obtain the organic key of high-purity (because the diffusion rate of impurity in solid phase is slower), and the steady flow of solid-liquid two-phase is the key that guarantees the operation of crystallizing tower continous-stable in the crystallizing tower.U.S. Pat 2659761 discloses a kind of fusion-crystallization method of purification, the corollary apparatus of this method is a kind of tower crystallizer, tower body is divided into reflux section and direct crystallization section, reflux section is positioned at tower body top, the direct crystallization section is positioned at the tower body bottom, double spiral agitator is delivered to the reflux section on crystallizing tower top with crystal from the crystallized region of crystallizing tower bottom, and phegma moves from top to bottom, and from bottom to top crystal is carried out countercurrent washing.The weak point of this patent is: 1) the easy crystallization dirt of crystallized region tower body outer casing inner wall.Because the crystallizer shell is a cylindrical shape, thereby the dead band is stirred in existence between the outer casing inner wall of double spiral agitator and tower body, stir the existence in dead band, the crystal that makes crystallized region tower body outer casing inner wall separate out can not be scraped by double spiral agitator in time, thereby crystal layer appears in the tower body outer casing inner wall herein, even the solid-liquid two-phase flow that the appearance of this crystal layer does not influence in the tower is moving, also can influence the heat transfer efficiency and the production capacity of device, after the long-play, when treating crystal bed length to certain thickness, will stop up crystallized region, make device can not continue operation; If it is loosening that crystal bed is scraped by double spiral agitator, fall down from the tower wall, then may block double spiral agitator, make device can not continue operation or influence washing refining effect.Simultaneously, intermittently scrape crystal block, can destroy the solid-liquid biphase equilibrium of having set up, make crystallizing tower not move continuously and stably from the tower body outer casing inner wall.2) be difficult to the counter-current flow that realizes that the solid-liquid two-phase is stable.For most organic systems, the density of solid-liquid two-phase differs seldom, moreover, in the fusion-crystallization process, crystal is to form in the fused solution of himself, crystal particles is very tiny, under the situation of stirring, in the fused solution around crystalline particle always can be dispersed in, be difficult to upwards be carried, therefore can not realize the counter-current flow that the solid-liquid two-phase is stable effectively, if will keep the stable counter-current flow of solid-liquid two-phase by double spiral agitator, then need crystal particles to grow up to certain size, thereby the crystallization time growth, the growth of crystallization time has not only increased energy consumption, and influence the production capacity of device, increase the probability that brilliant scar appears in crystallized region tower body outer casing inner wall.In addition, because the solid-liquid contact area of bulky grain crystal is less, its refining effect will be lower than the granule crystal.3) be difficult to prepare the high-purity organic matter.As mentioned above, the described device of this patent is wanted and can be operated by continous-stable, crystalline particle is grown up to certain size, but the sweating mechanism of purifying so just can not be fully used, causing purifies mainly relies on countercurrent washing, thereby is difficult to obtain the high pure organic matter more than 99.99%.4) energy consumption increases, and operation easier increases.Upwards carry the bulky grain crystal, increased power consumption on the one hand, on the other hand strict requirement has been proposed stir speed (S.S.), increased operation easier, stir speed (S.S.) is too low, then can not upwards carry crystal to realize that the solid-liquid two phase countercurrent flow flows, and stir speed (S.S.) is too high, then can make shortening time of contact of solid-liquid two-phase, not reach good clean result.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, a kind of device of preparing high pure organic matter by fusion-crystallization method is provided, this device can not only move by continous-stable, and can cut down the consumption of energy.
Technical scheme of the present invention: 1) change the crystallizing tower profile, eliminate and stir the dead band.2) crystallizing tower is divided into 3 sections, wherein the crystallisation by cooling section is positioned at tower body top, and the crystal melt zone is positioned at the tower body bottom, the tower body middle part is for separating rectifying section, make flowing of material identical with its natural characteristic, promptly crystal flows, and it is subjected to gravity direction consistent with institute, and bottom hot melt liquid upwards flows.
The device of preparing high pure organic matter by fusion-crystallization method of the present invention is a tower structure, by shell and be positioned at the parallel coupling spiral agitator I of two axis of shell, spiral agitator II and heater are formed tower body, spiral agitator I, spiral agitator II is connected with the transmission of driving mechanism, tower body is divided into the crystallisation by cooling section, separate rectifying section and crystal melt zone, the crystallisation by cooling section is positioned at tower body top, the crystal melt zone is positioned at the tower body bottom, separate rectifying section between crystallisation by cooling section and crystal melt zone, heater is installed in the crystal melt zone, two spiral agitators are installed in and separate rectifying section and crystallisation by cooling section, charging aperture is arranged on the crystallisation by cooling pars infrasegmentalis, products export after the purification is arranged on crystal melt zone bottom, and the residual liquid discharge mouth is arranged on crystallisation by cooling section top; In the crystallisation by cooling section, around the shell of tower body cooling jacket is installed, cooling jacket offers the cooling medium inlet and cooling medium exports; The shell of tower body intersects cylindrical shapes by two, two cylinders respectively with spiral agitator I, spiral agitator II coaxial line.
In order to realize goal of the invention better, the present invention has also taked following technical measures:
1, with tower body with respect to the vertical certain angle that tilts, the angle θ of inclination is 25～45 °, allows crystal move downward along the tower wall, promotes the sedimentation of tiny crystalline particle, obtains good effect of settling.
2, with the clearance control between tower body outer casing inner wall and the spiral agitator fin at 1～3mm, to guarantee that the crystal on the tower body outer casing inner wall can be scraped totally, eliminate the crystallization dirt effectively.
3, at the melt zone of tower body screen cloth is installed, this screen cloth is positioned under the heater, to prevent that not melting crystal stops up discharging opening.
4, whole crystallizing tower is incubated, with the shell and the cooling jacket coating heat-insulating material of tower body, to keep the required thermograde of purification in the crystallizing tower better.
The operating process of purifying plant of the present invention and purification mechanism are as follows:
Mixture to be separated enters crystallizing tower by charging aperture, enter the crystallisation by cooling section with moving upward from the heat fusing liquid at the bottom of the tower, the product component of being purified is separated out in the continuous crystallization of crystallisation by cooling section, and relies on the auxiliary conveying effect of self gravitation and spiral agitator I, spiral agitator II to enter the separation rectifying section; Crystal carries out sweating at the separation rectifying section and purifies, being carried out countercurrent washing by the fused solution from the crystal melt zone simultaneously purifies, the product component of being purified moves to the high-temperature region, bottom gradually at the separation rectifying section, along with the rising of temperature, intracrystalline impurity constantly melts, and to exosmosis, carrying out sweating purifies, simultaneously, crystal is constantly carried out countercurrent washing by the fused solution from the crystal melt zone, thereby the purity of crystal is more and more higher; Crystal is melted after entering the crystal melt zone, and a part is discharged as product, and a part is moved to cat head as phegma, and washing is from the crystal of crystallized region; The raffinate that produces in the purification process is discharged from the residual liquid discharge mouth in the crystallisation by cooling section.Crystallizing tower can continued operation, also can intermittently operated.
The temperature of crystallisation by cooling section is controlled by the temperature and the flow of cooling medium in the chuck, and cooling medium can be refrigerated brine or other cold-producing medium.The temperature of crystallisation by cooling section should be lower than the fusing point of the product component of being purified, and is higher than the fusing point that remains other component.During intermittently operated, after charging finished, the temperature of crystallisation by cooling section should slowly drop to the assigned temperature below the product component fusing point of being purified, and this assigned temperature is decided by the character of system to be separated, the purity and the output of product requirement.The temperature of crystal melt zone is controlled by heater, and heater can adopt hot fluid medium heating or electrical heating.
The present invention has following beneficial effect:
1, because the structure of device of the present invention has satisfied fusion-crystallization method purification mechanism---the requirement of recrystallization, countercurrent washing and sweating, particularly can make full use of sweating mechanism, thereby adopt device of the present invention that binary mixture, multicomponent mixture are separated and purify, all can obtain the high pure organic matter product of purity more than 99.99%.
2, because the improvement of device tower body shell shape of the present invention and crystallisation by cooling section, the rational deployment (make the suffered gravity direction of crystal flow direction and its consistent) of separating rectifying section, crystal fusion section, not only guarantee the continous-stable operation of purifying plant, and reduced energy consumption effectively.
3, use double spiral agitator, can prevent crystallization dirt on single spiral agitator, strengthen the moving stability of solid-liquid two-phase flow in the tower, guarantee that crystallizing tower can stable operation.
4, double spiral agitator mainly plays a part to disperse the solid-liquid two-phase, and crystalline particle is very tiny, thereby rotating speed is lower, and power consumption is few.
5, with crystallizing tower tower body inclination certain angle, can significantly improve the stable counter-current flow of solid-liquid two-phase in the tower, effectively improve and separate refining effect.
6, because rational design has been carried out in the gap between tower body outer casing inner wall and the spiral agitator fin, will be not on the tower body outer casing inner wall can incrustation, the continous-stable that helps purifying plant moves.
7, the melt zone at tower body is equipped with screen cloth, can prevent from not melt crystal and stop up discharging opening.
8, whole crystallizing tower is taked the insulation measure, helped keeping the required thermograde of purifying in the crystallizing tower.
9, purification operations is simple, both can continued operation, and also can intermittently operated.
10, device of the present invention is purified to organic separation good versatility, can not only separate and purification eutectic type organic system, also can separate purification solid solution type organic system.
Description of drawings
Fig. 1 is a kind of structure diagram of the device of preparing high pure organic matter by fusion-crystallization method of the present invention, and among the figure, a section is the crystallisation by cooling section, and the b section is for separating rectifying section, and the c section is the crystal melt zone;
Fig. 2 is the A-A profile of Fig. 1;
Fig. 3 is a kind of structural representation of screen cloth;
Fig. 4 is a kind of structural representation of driving mechanism;
Fig. 5 is a kind of structural representation of transmission.
Among the figure, organic matter products export, 14-screen cloth, 15-heater, 16-bearing, 17-motor, 18-decelerator that 1-shell, 2-spiral agitator I, 3-spiral agitator II, 4-cooling jacket, 5-cooling medium inlet, 6-residual liquid discharge mouth, 7-transmission, the outlet of 8-cooling medium, 9-charging aperture, 10-heat-insulating material, the outlet of 11-thermal medium, 12-thermal medium inlet, 13-are purified.
The specific embodiment
Embodiment 1: mix the purification of dichloro-benzenes multicomponent eutectic type system
The high-purity paracide is a kind of fine chemical product, also is a kind of important organic synthesis raw material, is got by the benzene oriented chlorination usually.The percetage by weight of present embodiment paracide in the mixed dichloro-benzenes coarse-grain that the benzene oriented chlorination makes is 65%, and all the other are o-dichlorohenzene and m-dichlorobenzene, needs further to purify.Mixing each component of dichloro-benzenes coarse-grain is isomer, and its physical property is as shown in table 1:
Table 1
| Fusing point ℃ | Boiling point ℃ | |
| Paracide | 53.09 | 174 |
| M-dichlorobenzene | -24.8 | 173 |
| O-dichlorohenzene | -17 | 180 |
As can be seen from Table 1, the boiling point that mixes each component in the dichloro-benzenes coarse-grain is very approaching, be difficult to separate purification with the method for rectifying, and their fusing point differs bigger, is fit to separate with the method for fusion-crystallization.
In the present embodiment, the structure of purifying plant is tower structure as shown in Figure 1, forms tower body by shell 1 and parallel coupling spiral agitator I2, spiral agitator II3 and the heater 15 of two axis that be positioned at shell, the high 1.2m of tower body, the angle θ that tilts with respect to vertical is 30 °.Tower body is divided into crystallisation by cooling section a, separates rectifying section b and crystal melt zone c, and the crystallisation by cooling section is positioned at top, and its length is 0.35m, the crystal melt zone is positioned at the bottom, its length is 0.1m, separates rectifying section between crystallisation by cooling section and crystal melt zone, and its length is 0.75m; Charging aperture 9 is arranged on the crystallisation by cooling pars infrasegmentalis, and the products export 13 after the purification is arranged on crystal melt zone bottom, and residual liquid discharge mouth 6 is arranged on crystallisation by cooling section top, as shown in Figure 1.The shell 1 of tower body intersects cylindrical shapes by two, two cylinders respectively with spiral agitator I2, spiral agitator II3 coaxial line, the internal diameter of two cylinders is 60mm, the gap between its inwall and the spiral agitator fin is 2mm, as shown in Figure 2.In the crystallisation by cooling section, around the shell of tower body cooling jacket 4 is installed, cooling jacket offers cooling medium inlet 5 and cooling medium outlet 8; At the crystal melt zone, heater 15 is installed, heater is a coil arrangement, the heating of employing hot fluid medium offers thermal medium inlet 12 and thermal medium outlet 11 on the shell of this section tower body, screen cloth 14 is installed under the heater 15, its shape is identical with shell 1, as shown in Figure 3.Spiral agitator I2, spiral agitator II3 are positioned at and separate rectifying section and crystallisation by cooling section, and its lower end is installed on the bearing 16, and its upper end is connected with the transmission of driving mechanism, and rotating speed is 8 rev/mins; Driving mechanism is made up of motor 17, decelerator 18 and gear driving pair 7, as Fig. 4, shown in Figure 5.The shell 1 and the cooling jacket 4 of tower body are coated with heat-insulating material 10, and heat-insulating material is an asbestos cloth.
During purification operations, will mix the dichloro-benzenes mixture earlier and be heated to 35 ℃, and send into the crystallizing tower charging aperture then continuously, and start stirring, the rotating speed of spiral agitator is 8 rev/mins.The initial temperature of crystallizing tower crystallisation by cooling section is 35 ℃, and after charging finished, the temperature of crystallisation by cooling section was reduced to 10 ℃ gradually by 35 ℃.The temperature of crystallizing tower crystal melt zone is 60 ℃.Crystallizing tower reaches after the predetermined Temperature Distribution, beginning continuous feed and discharging.Crystallizing tower through continuous operation reach stable after, the paracide purity of discharging at the bottom of the tower can reach 99.993%.
Embodiment 2: the purification of acrylic acid-propionic acid two-component solid solution-type system
Acrylic acid is a kind of important Organic Chemicals, also is important synthetic resin monomer.Often contain the minor by-products propionic acid in the synthetic acrylic acid, prepare high-purity propylene acid, need a spot of propionic acid in the products of separated.In present embodiment acrylic acid-propionic acid mixture, acrylic acid percetage by weight is 70%.The physical property of acrylic acid-propionic acid is as shown in table 2:
Table 2
| Fusing point ℃ | Boiling point ℃ | |
| Propionic acid | -20.5 | 141.15 |
| Acrylic acid | 12.5 | 141 |
As can be seen from Table 2, the boiling point of acrylic acid, propionic acid is basic identical, and it is bigger that fusing point differs, acrylic acid is heat-sensitive substance in addition, under 40 ℃, get final product polymerization reaction take place, can't use the method for rectifying to separate, so the fusion-crystallization method is the most effectual way of separating them.
In the present embodiment, the structure of purifying plant is identical with embodiment 1, and difference from Example 1 is that tower body is 45 ° with respect to the angle θ that vertical tilts, and the rotating speed of spiral agitator is 6 rev/mins.
During purification operations, earlier acrylic acid-propionic acid mixture is heated to 10 ℃, sends into the crystallizing tower charging aperture then continuously, and start stirring, the rotating speed of agitator is 6 rev/mins.The initial temperature of crystallizing tower crystallized region is 10 ℃, and after charging finished, the temperature of crystallized region was reduced to-10 ℃ gradually by 10 ℃.The temperature of crystallizing tower melt zone is 15 ℃.Crystallizing tower reaches after the predetermined Temperature Distribution, beginning continuous feed and discharging.Crystallizing tower through continuous operation reach stable after, the acrylic acid purity of discharging at the bottom of the tower can reach 99.992%.
Claims (9)
1, a kind of device of preparing high pure organic matter by fusion-crystallization method, be tower structure, form tower body by shell (1) and parallel coupling spiral agitator I (2), spiral agitator II (3) and the heater (15) of two axis that be positioned at shell, spiral agitator I, spiral agitator II are connected with the transmission (7) of driving mechanism, it is characterized in that:
Tower body is divided into the crystallisation by cooling section, separates rectifying section and crystal melt zone, the crystallisation by cooling section is positioned at tower body top, the crystal melt zone is positioned at the tower body bottom, separate rectifying section between crystallisation by cooling section and crystal melt zone, heater (15) is installed in the crystal melt zone, two spiral agitators are installed in and separate rectifying section and crystallisation by cooling section, charging aperture (9) is arranged on the crystallisation by cooling pars infrasegmentalis, products export after the purification (13) is arranged on crystal melt zone bottom, and residual liquid discharge mouth (6) is arranged on crystallisation by cooling section top;
In the crystallisation by cooling section, around the shell of tower body cooling jacket (4) is installed, cooling jacket offers cooling medium inlet (5) and cooling medium exports (8);
The shell of tower body (1) intersects cylindrical shapes by two, two cylinders respectively with spiral agitator I (2), spiral agitator II (3) coaxial line.
2, the device of preparing high pure organic matter by fusion-crystallization method according to claim 1 is characterized in that tower body is 25～45 with respect to the angle θ that vertical tilts.
3, the device of preparing high pure organic matter by fusion-crystallization method according to claim 1 and 2 is characterized in that the gap between tower body outer casing inner wall and the spiral agitator fin is 1～3mm.
4, the device of preparing high pure organic matter by fusion-crystallization method according to claim 1 and 2 is characterized in that the melt zone of tower body is equipped with screen cloth (14), and this screen cloth is positioned under the heater (15).
5, the device of preparing high pure organic matter by fusion-crystallization method according to claim 3 is characterized in that the melt zone of tower body is equipped with screen cloth (14), and this screen cloth is positioned under the heater (15).
6, the device of preparing high pure organic matter by fusion-crystallization method according to claim 1 and 2 is characterized in that the shell (1) of tower body and cooling jacket (4) are coated with heat-insulating material (10).
7, the device of preparing high pure organic matter by fusion-crystallization method according to claim 3 is characterized in that the shell (1) of tower body and cooling jacket (4) are coated with heat-insulating material (10).
8, the device of preparing high pure organic matter by fusion-crystallization method according to claim 4 is characterized in that the shell (1) of tower body and cooling jacket (4) are coated with heat-insulating material (10).
9, the device of preparing high pure organic matter by fusion-crystallization method according to claim 5 is characterized in that the shell (1) of tower body and cooling jacket (4) are coated with heat-insulating material (10).
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009026772A1 (en) * | 2007-08-24 | 2009-03-05 | Yibin Tianyuan Group Company Limited | Self-clearing reactor for preparing formic acid |
| CN102366679A (en) * | 2011-08-31 | 2012-03-07 | 华南理工大学 | Horizontal spiral push-type supersonic cooling crystallization machine |
| CN103086846A (en) * | 2011-10-28 | 2013-05-08 | 中国石油化工股份有限公司 | Apparatus and method for continuously separating isopropylphenol |
| CN104974062A (en) * | 2015-06-30 | 2015-10-14 | 成都理工大学 | TDI purification process of zone melting method |
| CN105061222A (en) * | 2015-09-01 | 2015-11-18 | 河北丰源环保科技股份有限公司 | 2, 4-diaminotoluene purification system |
| CN110152344A (en) * | 2019-07-02 | 2019-08-23 | 北京金隅琉水环保科技有限公司 | Mother liquor fine salt separator and mother liquid evaporation crystal system |
| CN110559681A (en) * | 2019-09-02 | 2019-12-13 | 湘潭大学 | Device and method for preparing high-purity p-cresol |
| EP2450338B1 (en) * | 2009-07-01 | 2020-02-12 | Nippon Shokubai Co., Ltd. | Process for production of (meth)acrylic acid |
| CN111544921A (en) * | 2020-06-29 | 2020-08-18 | 天津乐科节能科技有限公司 | Self-backheating continuous melting crystallization system and method |
| CN111905399A (en) * | 2020-08-31 | 2020-11-10 | 常熟龙飞医药设备科技有限公司 | Horizontal double-helix multistage countercurrent crystallization method and device |
| CN113318479A (en) * | 2021-06-04 | 2021-08-31 | 北京化工大学 | Continuous multi-stage countercurrent separation and purification device |
| CN115177970A (en) * | 2022-08-08 | 2022-10-14 | 上海交通大学 | Continuous multi-stage zone crystallization control device |
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| US2659761A (en) * | 1948-08-23 | 1953-11-17 | Dow Chemical Co | Fractional crystallization method |
| DE3049088A1 (en) * | 1980-12-24 | 1982-08-19 | Stohrer-Doduco GmbH & Co, 7250 Leonberg | Archimedean screw removes crystals deposited from electrolyte - continuously fed through externally cooled container |
| CN85203570U (en) * | 1985-08-22 | 1986-07-23 | 昆明工学院科研处 | Eutectic alloy crystallized with continual spiral rotation-liquated composite |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2009026772A1 (en) * | 2007-08-24 | 2009-03-05 | Yibin Tianyuan Group Company Limited | Self-clearing reactor for preparing formic acid |
| EP2450338B1 (en) * | 2009-07-01 | 2020-02-12 | Nippon Shokubai Co., Ltd. | Process for production of (meth)acrylic acid |
| CN102366679A (en) * | 2011-08-31 | 2012-03-07 | 华南理工大学 | Horizontal spiral push-type supersonic cooling crystallization machine |
| CN103086846A (en) * | 2011-10-28 | 2013-05-08 | 中国石油化工股份有限公司 | Apparatus and method for continuously separating isopropylphenol |
| CN103086846B (en) * | 2011-10-28 | 2015-08-19 | 中国石油化工股份有限公司 | A kind of device and method being continuously separated isopropyl-phenol |
| CN104974062A (en) * | 2015-06-30 | 2015-10-14 | 成都理工大学 | TDI purification process of zone melting method |
| CN105061222A (en) * | 2015-09-01 | 2015-11-18 | 河北丰源环保科技股份有限公司 | 2, 4-diaminotoluene purification system |
| CN110152344A (en) * | 2019-07-02 | 2019-08-23 | 北京金隅琉水环保科技有限公司 | Mother liquor fine salt separator and mother liquid evaporation crystal system |
| CN110559681A (en) * | 2019-09-02 | 2019-12-13 | 湘潭大学 | Device and method for preparing high-purity p-cresol |
| CN111544921A (en) * | 2020-06-29 | 2020-08-18 | 天津乐科节能科技有限公司 | Self-backheating continuous melting crystallization system and method |
| CN111544921B (en) * | 2020-06-29 | 2020-10-16 | 天津乐科节能科技有限公司 | Self-backheating continuous melting crystallization system and method |
| CN111905399A (en) * | 2020-08-31 | 2020-11-10 | 常熟龙飞医药设备科技有限公司 | Horizontal double-helix multistage countercurrent crystallization method and device |
| CN111905399B (en) * | 2020-08-31 | 2024-02-23 | 常熟龙飞医药设备科技有限公司 | Horizontal double-screw multistage countercurrent crystallization method and device |
| CN113318479A (en) * | 2021-06-04 | 2021-08-31 | 北京化工大学 | Continuous multi-stage countercurrent separation and purification device |
| CN115177970A (en) * | 2022-08-08 | 2022-10-14 | 上海交通大学 | Continuous multi-stage zone crystallization control device |
| CN115177970B (en) * | 2022-08-08 | 2023-08-08 | 上海交通大学 | Continuous multistage regional crystallization control device |
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