124results about "Crystallization regulation/control" patented technology

The invention provides a cooling rate optimization control method and system for continuous cooling crystallization, and the method comprises the steps: collecting crystal slurry concentration data and temperature data of each stage of crystallization tank in real time; the crystal slurry concentration data, the temperature data and the feeding flow data are input into a deep learning model, and a prediction result is obtained; based on the prediction result and crystal mush concentration data, dynamically adjusting the cooling rate of each stage of crystallizing tank and the addition amount of a co-crystallizing solvent; and feeding back an outlet crystal mush concentration signal of the last-stage crystallizing tank to the solid-liquid separation unit, and adjusting the running rotating speed of the solid-liquid separation unit in a linkage manner. According to the cooling rate optimization control method and system for continuous cooling crystallization, prospective correction of the cooling rate is carried out by using the predicted supersaturation degree, and adjustment of the additive amount of the auxiliary crystallization solvent is carried out by using the predicted crystal particle size distribution; and finally, an outlet concentration signal of the last-stage crystallizing tank is fed back to the solid-liquid separation unit in real time to adjust the separation rotating speed in a linkage manner, so that the crystal particle size deviation is reduced, and the triazole crystallization recovery rate is improved.

The invention relates to the technical field of mixing equipment, and discloses a mixing preparation device and method for a plant growth regulator containing a silicon element. The mixing preparation device of the silicon-containing plant growth regulator comprises a stirring main kettle, an online monitoring unit, a solid-liquid separation unit and a control unit, the stirring main kettle is used for carrying out a liquid-phase chemical reaction and separating out a solid product in situ, and is provided with a stirring piece; and the on-line monitoring unit is used for acquiring a reaction process signal and a crystallization state signal in the main stirring kettle in real time. The online monitoring unit, the solid-liquid separation unit and the control unit are arranged and cooperatively used, dynamic optimization management of the reaction crystallization process is achieved, the solid-liquid separation unit moves out crystals in time and circularly supplements materials, the problem that the crystals are secondarily wrapped is solved, meanwhile, reaction balance is pushed to move rightwards, and the reaction efficiency is improved. The conversion rate and the yield are improved.

According to the low-energy-consumption evaporating crystallizer, a single driving motor is adopted, a rotating shaft rod is used for simultaneously driving a scale scraping assembly arranged in an evaporating cylinder to conduct dynamic scale scraping and solution stirring, one end of the rotating shaft rod passes through a first transmission mechanism and a linkage shaft, and the other end of the rotating shaft rod is driven by a second transmission mechanism. A spiral separation assembly in the gas-liquid separation tank is driven by the direction conversion mechanism to rotate at a high speed so as to strengthen gas-liquid separation; and the other end of the discharging pipe drives a discharging assembly in the discharging pipe to rotate through a second transmission mechanism, so that discharging blockage prevention and negative-pressure deslagging are realized. Through a single power source, cooperative linkage of five functions of scale scraping, stirring, separation, blocking prevention and slag discharging is achieved, the structure is compact, the problems that traditional equipment is serious in scaling, poor in gas-liquid separation effect and prone to blockage during discharging are effectively solved, and meanwhile energy consumption of the equipment is remarkably reduced.

The invention relates to the technical field of ammonium dihydrogen phosphate preparation, and discloses a high-purity ammonium dihydrogen phosphate crystallization device and a method thereof.The high-purity ammonium dihydrogen phosphate crystallization device comprises a first-stage crystallization system, a first-stage centrifugal separation system, a second-stage crystallization system and a second-stage centrifugal separation system which are connected in series. The primary crystallization system comprises a crystal elimination heater, a crystal elimination mixer, a bag filter and a DTB flash cooling crystallizer which are connected in sequence, and is used for primarily purifying a concentrated solution; the primary centrifugal separation system is used for separating primary crystals; the second-stage crystallization system comprises a crystal dissolving tank, an OSLO cooling crystallizer and the like, and deep crystallization is carried out after the first-stage crystal is dissolved; the secondary centrifugal separation system is used for separating secondary crystals; through two-stage crystallization coupling, mother liquor graded circulation, a unique gradient washing process and active impurity control, efficient and continuous production of battery-grade ammonium dihydrogen phosphate with wet-process phosphoric acid as a raw material is realized, the product purity is high, the process flow is simplified, the cost is low, and the system operation is stable.

This application relates to the field of functional crystalline material preparation and microfluidic application technology, specifically disclosing a method and product for preparing formate crystals using core-shell microcapsules, including the following steps: (1) dissolving a solid alkaline raw material in a formic acid solution to prepare reaction solution a; (2) separately conveying polymer solution A and polymer solution B with phase separation characteristics, and reaction solution a, so that they are mixed at the intersection of microchannels to prepare dispersed phase b, which is then introduced into the assembly zone for phase separation assembly to form core-shell microcapsules; (3) the core-shell microcapsules are crystallized in a continuous temperature-changing crystallization zone to form formate solid; (4) the formate solid is collected, washed and dried sequentially to obtain the target product; (5) the oil layer is continuously extracted and returned to the assembly zone for recycling. The formate crystals prepared in this application not only have a large particle size, but also exhibit good size uniformity and morphological repeatability, and have the advantages of high throughput, green environmental protection, and simple operation.

The invention discloses a use method of 2, 4-dihydroxybenzoic acid dissolving and recrystallizing equipment, the 2, 4-dihydroxybenzoic acid dissolving and recrystallizing equipment comprises a closed dissolving kettle, a crystallization kettle and a mother liquor storage tank, the closed dissolving kettle, a first separator, a first filtrate storage tank and the crystallization kettle are connected in sequence, and the mother liquor storage tank is connected with a second separator. A discharge port of the crystallization kettle is connected with a feed port of a second separator, a filtrate discharge port of the second separator is connected with a liquid inlet of a second filtrate storage tank, and a liquid outlet of the second filtrate storage tank is communicated with a liquid inlet of the mother liquid storage tank through a third pipeline; the second pipeline between the first separation column and the second pump body is communicated with a liquid outlet of the mother liquid storage tank through a fourth pipeline; the second pipeline between the second pump body and the fourth pipeline is communicated with one end of a backflow pipeline, and the other end of the backflow pipeline is communicated with the first pipeline. The 2, 4-dihydroxy benzoic acid dissolving and recrystallizing equipment disclosed by the invention can be used for preparing 2, 4-dihydroxy benzoic acid with the purity of 99.68%, and the content of metal ions is reduced to 0.15 ppm.

Method for producing electronic grade nickel sulfate from nickel powder, crystallization apparatus, and control thereof The present invention provides a method for producing nickel sulfate, and nickel sulfate produced thereby. The process includes acid leaching, copper removal, acid adjustment, concentration, cooling crystallization, drying and sieving, and secondary leaching. Oxidation In the calcination furnace, the temperature is 400 to 700°C, and 1 kg of compressed air is used for each kilogram of nickel powder. ~5m 3 The reaction time is 1.0 to 2.5 hours, and the temperature during acid immersion is controlled to 45 to 70°C. Then, add dilute sulfuric acid to control the pH to 0.5-1.5 and react for 1-3 hours. The copper removal is to replace the copper with nickel powder, and the acid conditioning is to use nickel hydroxide or The pH is adjusted to 2.5-4.5 using nickel carbonate, and the filtrate is concentrated by The cooling crystallization method is to obtain nickel sulfate crystals and return the mother liquor to the concentrate. Drying and sieving is to add the undersieved material to the crystallizer as seed crystals, and secondary leaching is to Dilute sulfuric acid is added to the leaching slag, and it is reacted with nickel sulfate or hydrogen peroxide until nickel is less than 0.1%. If the first stage is full, the second leaching is continued. The crystallizer is a crystallizer that is connected in series with a second-stage crystallizer and a third-stage crystallizer. A crystallization frame, an oscillator provided under the crystallization frame, and an oscillator provided at the exit end of the crystallization frame. The crystallization frame is a rectangular parallelepiped. The bottom of the ribs are evenly spaced, with a cross section of a circular arc. The distance between two adjacent ribs is S is 1 / 25 to 1 / 15 of the width of the crystallization frame, and either the width b or the height h of the rib The width of the crystallization frame is 1 / 100 to 1 / 150 of the width of the crystallization frame. It does not add any new impurity ions, and does not add any oxidizing agent. The nickel sulfate crystal particles produced are uniform and are free of the static generation. This avoids caking of very large particles, irregularly shaped particles and crystals.

The present disclosure provides a preparation system and a preparation method for xylitol crystals. In the preparation system, outlets of a first centrifuge are connected with an inlet of a hot air drying tank and an inlet of a primary mother liquor storage tank through pipelines, respectively. Outlets of a second centrifuge are connected with an inlet of a second fluidized bed dryer and an inlet of a secondary mother liquor storage tank through pipelines, respectively. An outlet of a dicrystalline sugar dissolution tank is connected with an inlet of a blending tank through a pipeline. An outlet of a tricrystalline sugar dissolution tank is connected with the inlet of the primary mother liquor storage tank. The blending tank is provided with an inlet for a raw material of xylitol hydrogenation solution. An output of an outlet of a first fluidized bed dryer is prepared xylitol crystals.

The invention provides a cooling crystal obtaining system for generating a chelated fertilizer, and relates to the technical field of mixed fertilizer manufacturing, the cooling crystal obtaining system comprises a crystallization bin, the middle of the bottom of the crystallization bin is connected with a circulating pipeline, and the front side of the lower end of the circulating pipeline is connected with a discharge pipeline; a chelating bin is fixedly arranged at the top of the crystallizing bin, a top cover is fixedly arranged at the top of the chelating bin, and a feeding pipe is fixedly connected to the front upper part of the top cover; six groups of expansion grooves are integrally arranged below the outside of the chelating bin, and semiconductor refrigeration plates are fixedly arranged outside the expansion grooves; in the system, the chelating bin and the crystallizing bin continuously convey liquid materials through the air pressure and communicating vessel principle, circulating backflow retreatment of the uncrystallized liquid materials is achieved through the circulating device, the flow direction of the liquid materials is accurately regulated and controlled in cooperation with the electric cylinder A and the electric cylinder B, and the whole process of raw material supplementation, crystal generation and crystal separation can be completed without shutdown; the problems that traditional evaporative crystallization is low in efficiency and continuous operation cannot be achieved are solved, and the yield of chelated fertilizer crystals in unit time is remarkably increased.

The application discloses a kind of phosphoric acid extraction semi-water-two water alternate crystallization system and method, belong to the technical field of wet-process phosphoric acid production, the system is by the reaction tank unit of series connection and semi-water and two water reaction tank alternate arrangement, with the sulfuric acid dilution mixed heat exchanger group connected with reaction tank, simple heat exchanger group is arranged between tank to realize heat transfer.Construction.The method includes: material is temperature-adjusted after passing through sulfuric acid dilution mixed heat exchanger, in turn into the reaction tank sequence of alternate arrangement, heat circulation is carried out in adjacent tank by simple heat exchanger, under the control of PLC in 75~85 DEG C and 88~95 DEG C interval, realize the alternate crystallization of semi-water-two water calcium sulfate.The application replaces traditional flash evaporation external discharge with heat internal circulation between tank, solves the technical problems of high steam energy consumption, low phosphorus recovery rate, insufficient phosphoric acid concentration and high upgrading cost of stock device in traditional process, and has the comprehensive advantages of energy saving, yield, low-cost transformation and phosphogypsum resource.

The invention relates to a eutectic freeze crystallization apparatus of liquid, comprising: a eutectic freeze crystallization chamber (200) comprising an internal space having a first portion and a second portion and configured to receive said liquid via a feeding inlet arranged within the eutectic freeze crystallization chamber; mixing means arranged within the internal space at the first portion and configured to mix the liquid therein; a cooling element configured to cool the liquid within the internal space for lowering temperature of the liquid such that ice and salt crystals will be formed within the liquid; and conveyor means extending at least within the internal space and configured to convey at least part of the ice and salt crystals from the liquid towards a first outlet arranged at the second portion and to feed out via the first outlet the at least part of the ice and salt crystals from the internal space of the eutectic freeze crystallization chamber. The ice and salt crystals are separated in a separation unit (333).

The present application relates to a kind of device and method for extracting high-purity chemicals from coal tar wash oil fraction, comprising: naphthalene separation column, methylnaphthalene separation unit, acenaphthene-fluorene-dibenzofuran separation unit;Methylnaphthalene separation unit includes methylnaphthalene separation tower, β-methylnaphthalene subunit and α-methylnaphthalene subunit connected in sequence;Acenaphthene-fluorene-dibenzofuran separation unit includes light removal tower, acenaphthene subunit, dibenzofuran subunit and fluorene subunit connected in sequence;The material outlet of the bottom of naphthalene separation column is connected with methylnaphthalene separation tower;The material outlet of the bottom of methylnaphthalene separation tower is connected with the material inlet of light removal tower.The device provided by the present application can effectively extract target chemicals in coal tar wash oil fraction by reasonable configuration of the device and coupling cooperation between devices, and obtain high-purity products.Compared with existing wash oil extraction chemical technology, it has higher efficiency, wider applicability and better product quality.

The invention relates to the technical field of salt preparation systems, in particular to a sodium chloride and sodium sulfate large-particle salt preparation system, which comprises a crystallization separation module, a sodium chloride and sodium sulfate large-particle salt preparation module and a sodium chloride and sodium sulfate large-particle salt preparation module, the fine crystal elimination and crystallization module comprises a crystal grading and growing kettle, a thickener and a centrifugal machine, a solution is evaporated and crystallized through the crystal separation module and conveyed to the fine crystal elimination and crystallization module, and the fine crystal elimination and crystallization module carries out grading and growing on the solution and forms crystals with different particle sizes; and the floating fine crystal is conveyed to the fine crystal eliminating and dissolving module again to carry out fine crystal dissolving on the unsaturated solution, the dissolved solution is conveyed to the fine crystal eliminating and crystallizing module again, and after the sinking particle crystal is thickened, centrifugal dewatering is carried out to form a crystal with a large crystal form particle size and a large crystal form particle size. And the crystal is round and regular in morphology, so that the crystal is good in flowability, anti-caking, high in strength and not easy to break, and industrial subsequent treatment is greatly reduced.

The invention provides a novel production method of pentaerythritol, which relates to the technical field of chemical products, and comprises the following steps: proportioning formaldehyde, acetaldehyde and lithium hydroxide, mixing, carrying out condensation reaction, and adding formic acid to neutralize the solution after the reaction; collecting the neutralized solution, carrying out rectification treatment, and separating out crystals; carrying out centrifugal treatment on the separated crystals, and then putting the crystals into a washing tank for washing; drying to obtain a pentaerythritol finished product; precipitating the mother liquor, washing and refluxing the filtered solution, and mixing the filtered solution with the dealdehyding solution for cyclic utilization; and concentrating, crystallizing, centrifuging, washing and drying the filtrate to obtain a lithium formate product. According to the production method of the pentaerythritol by the lithium method, the reaction conversion rate is high, and the product quality is excellent; the added value is high, and the overall economy of the production process is good; the mother liquor is completely circulated in a closed manner, and is pollution-free and environment-friendly. The automation degree is high, and the washing, overturning and discharging processes can be completed only through single power equipment.

This invention discloses an ultrasonic-cold finger coupled plate melt crystallizer and a continuous purification process. The crystallizer body includes multiple heat exchange plates, each with a built-in serpentine refrigerant channel; multiple ultrasonic vibrating plates are sequentially arranged around the shell of the plate melt crystallizer to provide an ultrasonic field covering the entire crystallizer body; at least one cold finger assembly is located on top of the plate melt crystallizer and connected to the upper cover plate of the crystallizer body via a detachable flange. The cold finger assembly includes an inlet manifold, an outlet manifold, a cold finger body, and an ultrasonic probe. The inlet and outlet manifolds are arranged parallel to each other above the crystallizer body along a second direction. The bottom of each cold finger body is located within the crystallizer body, and its top two ends are connected to the inlet and outlet manifolds, respectively. The ultrasonic probe extends along a third direction and is inserted into the interior of the cold finger body. Using the melt crystallizer and process of this invention enables higher crystallization efficiency and greater product yield.

The application discloses a potassium dihydrogen phosphate solution cooling crystallization device and a use method thereof, and belongs to the technical field of crystallization devices. The device comprises a cooling cavity, a cooling pipe arranged at the central bottom of the cooling cavity, two turning plates, a push rod, a power source and two connecting rods. The two turning plates are respectively arranged at the two sides of the cooling pipe and are hingedly connected with the inner bottom of the cooling cavity. The two sides of the two turning plates are sealingly matched with the inner side wall of the cooling cavity. The one end of the connecting rod is connected with the other end of the turning plate. The power source is fixedly connected with the outer wall of the cooling cavity and is drivingly connected with the other end of the push rod. The two connecting rods are symmetrically fixedly connected with the inner top of the cooling cavity. The triangular cooling cavity is hingedly connected with the free end of the connecting rod, so that the longest side of the triangular cooling cavity is adjacent to the turning plate. The feeding port is arranged in the central top region of the cooling cavity. The application has the beneficial effects of improving the cooling effect, shortening the cooling time and improving the quality of the generated potassium dihydrogen phosphate crystal.

The invention discloses an experimental device for a drug crystallization process. The experimental device comprises a reactor, a lifting probe assembly, a crystallization guide assembly and a control system. The reactor comprises a reaction kettle and a heating base which are in heat conduction connection; the lifting probe assembly is mounted on the reaction kettle and can extend below the liquid level to shoot crystal images; the crystallization guide assembly comprises a rotary driving mechanism, a shaft tube, a first ultrasonic transducer, a second ultrasonic transducer, a focused light beam reflection measuring instrument, a turbidity sensor and a stirring piece; wherein the frequency of the first ultrasonic transducer is lower than that of the second ultrasonic transducer, and the first ultrasonic transducer and the second ultrasonic transducer are used for inducing nucleation and fine grain elimination; the focused beam reflection measuring instrument monitors the number and granularity of crystals; the heating base, the lifting probe assembly, the rotary driving mechanism, the first ultrasonic transducer, the second ultrasonic transducer, the focused light beam reflection measuring instrument and the turbidity sensor are all electrically connected with the control system, so that monitoring and control of the experiment process are realized, the crystallization efficiency is effectively improved, and high-quality crystals are obtained.

The application discloses a method for digesting and separating fluorinated aluminum by program, which comprises the following steps: placing a catalyst with metal elements supported on alumina as a carrier into a reaction container of a cluster digestion device, adding hydrochloric acid and / or nitric acid, setting a digestion program, introducing inert gas for pre-pressurization, performing primary digestion, and simultaneously starting a condensation reflux atomizer; after the program is completed, adding hydrofluoric acid, setting a digestion program, and performing secondary digestion; after the digestion is completed, entering a cooling and crystallization program, performing cooling and crystallization, and separating to obtain a sample solution to be detected and a solid; the solid is dried and calcined to obtain fluorinated aluminum crystals, and the liquid is used for detecting the content of metal elements. The method is applied to the digestion treatment of the alumina sample with metal elements supported thereon, has a large sample treatment range, complete digestion, no volatile loss of elements, and can separate AlF3 in an alpha crystal form through the program digestion of the digestion device.

The invention relates to the technical field of industrial high-salinity wastewater treatment and recycling, and discloses a sodium sulfate evaporative crystallization process for treating comprehensive wastewater of a steel mill, which comprises the following steps: S1, performing multi-effect evaporation concentration on sodium sulfate concentrated water generated by the comprehensive wastewater of the steel mill after pretreatment and membrane separation concentration, sodium sulfate concentrated crystal mush is obtained; s2, carrying out solid-liquid separation on the sodium sulfate concentrated crystal mush to obtain sodium sulfate crystals and mother liquor; part of the mother liquor returns to the system to participate in circular evaporation and concentration; and S3, monitoring the concentration of the mother liquor which is circularly evaporated in the step S2, and executing intermittent mother liquor discharge based on a performance attenuation signal of the evaporation system. Through a composite process route of multi-effect evaporative crystallization, freezing crystallization, advanced oxidation and membrane separation, comprehensive steel mill wastewater with complex components and high organic matter content is successfully treated, a high-quality anhydrous sodium sulfate product is produced, and zero discharge of wastewater and recovery of valuable resources are realized.

This invention belongs to the technical field of anthracene oil processing and production, and discloses a production method for increasing the anthracene and carbide content in crude anthracene products using crystal nucleus seeds. The method mainly involves cooling the heated raw anthracene oil to 75°C, then adding high-quality crystal nucleus seeds (70% anthracene content, 17% carbide content, and ≤1% mechanical impurities) to a crystallization tank at a mass ratio of 1:75. At this point, the high-quality crystal nucleus seeds promote the formation of new crystal nuclei in the anthracene oil liquid. As the temperature decreases, the newly formed crystal nuclei gradually grow. Simultaneously, the temperature is naturally lowered to below 65°C through stirring, and the cooling system in the crystallization tank is activated to further cool the temperature to 35-40°C. The mixture is then repeatedly fed and dried in a centrifuge to produce high-quality crude anthracene. This invention utilizes unique high-quality crystal nucleus seeds to achieve an anthracene content of over 40% and a carbide content of over 14% in crude anthracene even when the anthracene and carbide content in the raw anthracene oil is low or unstable, resulting in a superior-grade crude anthracene product.

The disclosure relates to methods for crystallization of active pharmaceutical ingredients (APIs), wherein the crystallization and crystal growth is controlled. According to the method solid amorphous nanosized API and an aqueous solution comprising one or more polymers and / or copolymers are contacted so as to form a suspension comprising nanosized API in crystalline form.

A crystallizer modeling method according to an embodiment of the present disclosure may comprise the steps of: calculating a first stress distribution of a first crystallizer; setting a parameter required for modeling a second crystallizer scaled down from the first crystallizer; calculating a second stress distribution of the second crystallizer on the basis of the set parameter; comparing the second stress distribution with the first stress distribution; determining a parameter for calculating a second stress distribution matching the first stress distribution; and designing the second crystallizer on the basis of the parameter.

The invention provides a method and a system for obtaining a representative particle size of particles generated in a crystallization device. The present invention addresses the problem of obtaining a method for obtaining the particle size of particles generated in a crystallization device from the turbidity, the concentration of the particles generated, and the supply amount of a starting material using a single correlation formula during the crystallization process. In the present invention, a correlation formula for the variables is created in advance from the representative particle size of the particles, the turbidity of the dispersion of the particles, the concentration of the particles in the dispersion of the particles, and the basic data of the amount of metal supplied from the metal salt, which are acquired by a particle size distribution measurement device. The representative particle size of the generated particles is obtained from the turbidity obtained by measuring the dispersion of the generated particles, the concentration of the generated particles, and the supply amount of the metal from the metal salt by using the correlation formula.

The invention relates to a eutectic freeze crystallization apparatus of liquid, comprising: a eutectic freeze crystallization chamber comprising an internal space having a first portion and a second portion and configured to receive said liquid via a feeding inlet arranged within the eutectic freeze crystallization chamber; mixing means arranged within the internal space at the first portion and configured to mix the liquid therein; a cooling element configured to cool the liquid within the internal space for lowering temperature of the liquid such that ice and salt crystals will be formed within the liquid; and conveyor means extending at least within the internal space and configured to convey at least part of the ice and salt crystals from the liquid towards a first outlet arranged at the second portion and to feed out via the first outlet the at least part of the ice and salt crystals from the internal space of the eutectic freeze crystallization chamber.

The invention relates to a method for initiating the crystallization of a solute present in a solution (S) at a concentration that makes it metastable, comprising the application of one or more plasma pulses to the solution (S).

Systems and methods for preparing compound crystals of erythritol and high-intensity sweeteners are provided. The systems may comprise a fermentation liquid storage tank (1), a ceramic membrane filtration system (2), a nanofiltration system (3), a first evaporator (4), a first crystallization kettle (5), a first centrifuge (6), a sugar dissolution tank (7), a decolorization tank (8), an ion exchange column (9), a blending tank (10), a second evaporator (11), a second crystallization kettle (12), a second centrifuge (13), a hot-air drying tank (14), a fluidized drying bed (15), and a finished product tank (16) sequentially connected through pipelines. The systems may further comprise a high-intensity sweetener storage tank (17), a primary mother liquor tank (18), and a secondary mother liquor tank (19). The finished product tank (16) may store a prepared compound crystallization product of the erythritol and the high-intensity sweetener.

The present application relates to a kind of large particle size sodium nitrate multistage flash cooling crystallization production systems, it includes feed unit, evaporation unit, seed unit, flash crystallization unit, condensation unit, thickening unit, centrifugal drying unit and mother liquor reflux unit, seed unit includes material pump and seed tank, the discharge port of separator is connected to seed tank by material pump;Flash crystallization unit includes first flash crystallization ware, first material pump, second flash crystallization ware, second material pump, third flash crystallization ware and third material pump, the discharge port of seed tank is connected to the feed port of first flash crystallization ware, first flash crystallization ware, second flash crystallization ware, third flash crystallization ware are sequentially connected.The sodium nitrate solution of the present application is distributed uniformly by multistage flash, crystal growth time, and crystal size is adjusted by controlling fine crystal elimination amount, crystal size is large, particle size distribution is uniform, crystal size D90≥0.9mm, variation coefficient CV≤25.

The application discloses a kind of continuous equipment and preparation method for coproduction fumaric acid and malic acid, the continuous equipment includes raw material tank, feed pump, layer type multistage overflow reaction tower, material pressure regulating valve, material tank, separator, crystallizer, washing crystallizer group, dryer and drying tower group, the preparation method for coproduction fumaric acid and malic acid is that raw material succinic anhydride, warm water and ionic liquid catalyst are 50-30:20:1-2 according to mass ratio in above-mentioned continuous equipment are processed after being fed, reaction, separation, purification, crystallization, drying, and high-purity fumaric acid and malic acid are obtained.The ionic liquid catalyst is used in succinic anhydride coproduction fumaric acid and malic acid reaction for the first time in the application, and continuous production equipment is designed, need not evaporation concentration and can be directly cooled crystallization, can greatly shorten reaction time, reduce energy consumption and production cost, and solve the technical problems, such as the difficulty of continuous production, preparation process complexity, catalyst recycling difficulty and the like in existing preparation method.

The invention relates to the technical field of pharmaceutical preparations, in particular to a freeze-drying process of mycophenolate mofetil for injection, which comprises the following steps: cooling a mycophenolate mofetil injection to-35 DEG C to-45 DEG C, carrying out primary heat preservation, tempering and heating to-10 DEG C to-5 DEG C, carrying out secondary heat preservation, cooling to-40 DEG C to-50 DEG C, carrying out third heat preservation, and carrying out freeze-drying under the condition that the vacuum degree is 25-35Pa, so as to obtain the mycophenolate mofetil for injection. And heating the pre-frozen solid to-25 DEG C to-15 DEG C, preserving heat for four times, heating to 35-45 DEG C, and preserving heat for five times to obtain the freeze-dried mycophenolate mofetil for injection. Through the freeze-drying process, the total impurity content of a freeze-dried product is smaller than or equal to 0.15%, the medication safety and stability are remarkably improved, and the one-time sublimation drying time is greatly shortened to 9 h from 16 h in a traditional process; meanwhile, the residual moisture of the finished product is controlled to be about 0.1%, and the finished product can be stored at room temperature and meets the requirements of industrial large-scale production.

This invention discloses a purification device and process for 1,3-dimethylimidazolinone based on coupled cooling, belonging to the field of chemical purification technology. It includes a main coupling unit and a membrane-assisted impurity removal unit. The main coupling unit comprises a vacuum distillation kettle and a three-stage cooling crystallization device. The vacuum distillation kettle utilizes a reduced-pressure environment to lower the boiling point of 1,3-dimethylimidazolinone (DMI), combined with the efficient mass transfer effect of θ-ring corrugated packing, to separate low-boiling substances, such as formaldehyde, from high-boiling residues, and initially enrich DMI vapor. The three-stage cooling crystallization device uses a gradient temperature field to achieve stepwise crystallization based on the melting point difference between DMI and impurities: primary crystallization preferentially separates high-purity DMI, while secondary and tertiary crystallization recover residual DMI and retain impurities, with real-time removal of crystals to prevent co-crystallization. The final product has high purity and a higher yield than traditional distillation. Vacuum distillation lowers the operating temperature, and combined with gradient crystallization, reduces repeated distillation, thus lowering overall energy consumption.