166results about "Product crystals bed crystallization" patented technology

The invention provides a method for recovering a BHET monomer from a waste polyester textile alcoholysis solution, and is characterized in that the recovery method comprises the following steps: (1) filtering: mixing the waste polyester textile alcoholysis solution with water under a stirring condition, and filtering at 55-70 DEG C; and (2) cooling crystallization: under a stirring condition, carrying out primary cooling on the filtrate obtained by filtering in the step (1) from 55-70 DEG C to 45-55 DEG C, then adding a BHET seed crystal, then carrying out secondary cooling to 5-15 DEG C, and maintaining the temperature for 20-60 min to obtain the BHET monomer. The mixed solution cooling crystallization method is developed on the basis of complexity of components of the waste polyester textile fabric, the problems that in the conventional production process, a BHET crystal product is low in quality, prone to scaling, difficult to filter and dry and the like are solved, and the obtained BHET product is large in particle size, narrow in particle size distribution, high in purity, good in fluidity and high in stability.

Disclosed are an aluminum diethylphosphinate crystal with a low fine powder content, a preparation method therefor and use thereof in flame retardance of glass fiber-reinforced engineering plastics. In the present invention, a phosphorus-containing aluminum salt complex is used as a seed crystal and is added in a crystallization process of preparing aluminum diethylphosphinate, such that the crystallization process can be effectively regulated and controlled, aluminum diethylphosphinate crystal particles with a low fine powder content, narrow distribution and a large particle size can be obtained, and the problems that the existing aluminum diethylphosphinate powder is prone to bridging, unsmooth feeding and the like can be solved. The present application is applicable to a processing technology of halogen-free flame retardant glass fiber-reinforced engineering plastics. The prepared aluminum diethylphosphinate includes a small amount of phosphorus-containing aluminum salt complex seed crystals, and the flame retardant property of the aluminum diethylphosphinate is not affected.

The invention belongs to the technical field of biological medicine, and particularly relates to sterile cefepime hydrochloride and a direct preparation method thereof. The method comprises the following steps: firstly, carrying out condensation reaction on a 7-MPCA solution and an AE active ester solution through a solid base catalyst column at the same time; then, carrying out extraction phase separation, two times of pH regulation crystallization, activated carbon decoloration and sodium sulfite reduction on the condensation liquid to obtain a cefepime hydrochloride liquid to be crystallized; and then taking a part of the cefepime hydrochloride to-be-crystallized liquid to prepare a seed crystal mixed liquid, and adding the rest of the cefepime hydrochloride to-be-crystallized liquid and the crystallization solvent into the seed crystal mixed liquid at a specific speed to obtain the sterile cefepime hydrochloride. According to the method disclosed by the invention, the continuous production of the sterile cefepime hydrochloride is realized, the preparation period of the sterile cefepime hydrochloride is greatly shortened, side reactions and product degradation are reduced, the quality and yield of the obtained cefepime hydrochloride product are relatively high and stable, and industrial production is facilitated.

Provided is a method of recovering valuable materials that is a method of recovering lithium carbonate from a lithium-ion secondary battery, where the lithium carbonate has a boron content of less than 1 ppm and a calcium content of 100 ppm or less. The method includes a heat treatment step, a crushing and classification step, a slurry formation step, a wet magnetic separation step, an acid leaching step, a neutralization step, a neutralized cake solid-liquid separation step, a calcium carbonate crystallization step, a calcium carbonate solid-liquid separation step, and a calcium adsorption and removal step.

A method of making colloidal kagome superlattices can include functionalizing a plurality of metal nanoparticles with a plurality of oligonucleotides to produce programmable atom equivalents; and cooling the programmable atom equivalents to induce crystallization of the programmable atom equivalents. The cooling process can include cooling the PAEs from a first temperature to a second temperature at a first cooling rate, cooling the PAEs from the second temperature to a third temperature at a second cooling rate, and cooling the PAEs from the third temperature to a fourth temperature at a third cooling rate. The kagome superlattices can have a rhombohedral unit cell formed by alternating chiral layers of PAEs organized in 2-dimensional distorted kagome layers. The colloidal superlattices can have anisotropic light emission, Purcell factors of at least 25 and birefringent properties.

The embodiment of the invention provides a crystallization promoter, a preparation method thereof and a wastewater treatment device. The crystallization promoter is used for removing target ions in wastewater, and comprises a slide glass, the density of which is smaller than that of the wastewater; and the seed crystal is arranged on the surface of the slide glass and is used for promoting the target ions to form crystals. The crystallization promoter can reduce the energy consumption of a wastewater treatment device.

Described are liquid compositions that contain a desired (e.g., extracted) plant material such as cannabinoid, terpene, terpenoid, or the like, contained, e.g., dissolved, suspended, or emulsified, in the liquid, which contains surfactant; methods of preparing these types of liquid compositions; and methods of processing this type of liquid composition to collect, isolate, concentrate, or purify a desired target material contained in the liquid composition.

The invention discloses a method of a calcium fluoride crystallization system based on a functional quartz sand coupled fluidized bed, which comprises the following steps: S1, pretreating quartz sand by using sodium hydroxide, and reacting silicon hydroxyl with silicon dioxide in the quartz sand by using KH550 as a silane coupling agent; and step S2, grafting a high-molecular organic monomer 2-acrylamido-2-methylpropanesulfonic acid on the KH550 in the step S1, and carrying out negative charge electricity modification. The fluorine ions in the fluorine-containing wastewater form calcium fluoride crystals through the fluidized bed, calcium fluoride is captured in situ through functional quartz sand, heterogeneous crystallization of calcium fluoride is enhanced, the filterability of precipitation particles is improved, calcium fluoride is captured in a resource mode while deep fluorine removal is achieved, the removal efficiency of the fluorine ions can be improved, and the method is suitable for industrial production. The fluorine concentration of the discharged water is reduced, the problem that follow-up agent adding is needed due to high turbidity of the discharged water of a traditional fluidized bed crystallizer is solved, the sludge yield is reduced, and the economical efficiency and sustainability of wastewater treatment are improved.

Payload systems for processing chemical substances under various gravity levels, such as hypergravity and / or microgravity. The payload systems may include a hypergravity thermal payload system configured to enable melt or cooling of a sample under hypergravity. Alternatively, or in addition, the payload systems may include a gravity-independent thermal payload system for enabling melt or cooling of a sample under various gravity levels, such as microgravity. Alternatively, or in addition, the payload systems may include a hypergravity crystallization payload system configured to enable crystallization of a chemical substance under hypergravity. Alternatively, or in addition, the payload systems may include a gravity-independent crystallization system configured to enable crystallization of a chemical substance in various gravity levels, such as microgravity.

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.

Processes and systems for preparing lithium carbonate with energy recovery. Various fluid streams are directed to one or more energy recovery devices to improve energy efficiency and system performance during lithium carbonate production. Lithium in a saltwater is extracted by applying direct lithium extraction to produce a lithium recovery solution. The lithium recovery solution is concentrated by a membrane concentrator and heated, and chelating ion exchange is used to purify the heated lithium recovery solution by removing multivalent cations and / or boron from it. The concentrated and purified lithium recovery solution is then reacted with sodium carbonate at a temperature of at least 70 °C to produce a lithium carbonate slurry, which is separated into lithium carbonate solids and a mother liquor. Prior to purification, the concentrated lithium recovery solution is heated using heat from at least one of the unconcentrated lithium recovery solution or the mother liquor.

A liquid separation method (10) for separating mono ammonium phosphate ("MAP") (20) in aqueous solution, includes: • a receiving step in which a process liquid which comprises water and MAP is received; • a cooling step in which a controlled cooling process is applied to the process liquid to induce the crystallization (14) of MAP; • a separating step (16) in which the crystallised MAP is separated from the remaining process liquid.

The invention relates to the technical field of purification of beta-alanine, and discloses a method for separating and purifying beta-alanine from fermentation liquor. The invention provides a method for separating and purifying beta-alanine from fermentation liquor by combining flocculation and resin to overcome the defects that an existing process for separating and purifying beta-alanine from fermentation liquor is tedious in route, high in cost and technology, large in energy consumption and the like. Impurity substances can be effectively removed through the steps of flocculation impurity removal, protein removal, resin adsorption decoloration, resin adsorption elution refining and crystallization extraction of beta-alanine, and the obtained product is high in purity. Meanwhile, the method is simple to operate, mild in process condition and low in cost.

The invention discloses a processing method for fractionation and rapid crystallization of palm oil, which comprises the following steps: (1) heating and controlling a palm oil raw material to be fractionated to 55-65 DEG C (crystal breaking), pumping the palm oil raw material into a crystallizing tank, and then cooling the palm oil raw material to about 25 DEG C under the action of rapid cooling of cooling water (or chilled water) and stirring; (2) continuously reducing the temperature of the palm oil raw material in the crystallizing tank by using chilled water, adding a certain proportion of palm oil (solid-liquid mixture) which is completely crystallized and is in an unseparated state into the crystallizing tank at the interval of 25.0-18.0 DEG C as a seed crystal, and controlling the stirring speed of the crystallizing tank at 15-30r / min until the palm oil raw material is completely cooled and crystallized; (3) after crystallization is completed, if seed crystals need to be added into the crystallizing tank which is cooling and crystallizing, pumping the seed crystals into the crystallizing tank which needs to be added with the seed crystals through a pump; otherwise, immediately pumping into a membrane filter for filtering and separating (preventing the tank from being burnt) to obtain liquid oil and stearin. The palm oil seed crystal is added, so that the crystallization time can be shortened; and through seed crystal induction, the formation of stable-form crystals is accelerated, excessive crystallization is avoided, and the interception loss of filtration is reduced, so that the liquid oil yield is improved.

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 discloses a method for separating high-purity chlorogenic acid and neochlorogenic acid from a stevia rebaudiana chlorogenic acid product based on membrane coupling extraction crystallization. The method comprises the following steps: preparing a first to-be-treated solution by taking the stevia rebaudiana chlorogenic acid product as a raw material; treating the first to-be-treated liquid through an ultrafiltration membrane and a nanofiltration membrane in sequence to obtain a trapped fluid II, concentrating the trapped fluid II, and adjusting the pH value to obtain a second to-be-treated liquid; extracting the second to-be-treated liquid with an ethyl acetate-n-butyl alcohol saturated aqueous solution to obtain a raffinate phase I and an extract phase I; adjusting the pH of the raffinate phase I to obtain a third to-be-treated solution; extracting the third to-be-treated liquid with an ethyl acetate-n-butyl alcohol saturated aqueous solution to obtain a raffinate phase II and an extract phase II; drying the extract phase I, crystallizing, pulping and purifying to obtain high-purity chlorogenic acid; and drying the extract phase II, crystallizing, pulping and purifying to obtain the high-purity neochlorogenic acid. According to the method, membrane separation, solvent extraction and fractional crystallization are coupled, and high-efficiency and high-selectivity separation and purification of chlorogenic acid and neochlorogenic acid in a stevia rebaudiana chlorogenic acid product are realized.

A method of manufacturing a particulate transition metal carbonate material is described. The method includes mixing a transition metal precursor salt with a second salt in a liquid vehicle. A precipitation reaction is then performed to form a slurry of the particulate transition metal carbonate material in the liquid vehicle. The particulate transition metal carbonate material may find use as seeds in a subsequent precipitation reaction. Methods of manufacturing a particulate precursor materials are also described, including performing a precipitation reaction between one or more transition metal sources in the presence of seed particles in a reaction mixture within a precipitation reaction vessel, to form the particulate precursor material by precipitation onto the surface of the seed particles.

The present technology relates to a process useful for preparing the crystalline (S)-1,1-bis(4-fluorophenyl)propan-2-yl (3-acetoxy-4-methoxypicolinoate)-L-alaninate compound (I), which comprises distilling a mixture, which comprises distilling a mixture containing an aprotic organic solvent, a protic organic solvent, the compound (I), and a seed crystal of the compound (I), or which comprises distilling a mixture containing an aprotic organic solvent and the compound (I) and crystallizing the compound (I) by preparing a second mixture containing a protic organic solvent, the compound (I), and a seed crystal of the compound (I). The process disclosed herein describes a more stable and storage-compatible preparation of the compound (I). Preparations of the compound (I) having fewer (trace) impurities are also disclosed.

A process and a chemical production unit for producing crystalline ammonium chloride in the presence of a crystallization additive are provided, wherein the process comprises the steps a) reacting NH3 and HCl by feeding NH3 and HCl to an aqueous solution of ammonium chloride; b) crystallizing ammonium chloride from the aqueous ammonium solution obtained in step a), and c) separating the crystalline ammonium chloride, wherein energy required in step b) is generated in step a). The crystalline ammonium chloride, obtainable by said process, is suitable as a flavoring agent, as an animal feed additive, as an additive for a cosmetic composition or as an additive for a pharmaceutical composition.

This invention provides a production process for manufacturing metallic magnesium and industrial silicon by decomposing serpentine using the hydrochloric acid method. [Solution] The present invention provides a method for processing serpentine ore as a raw material using a two-stage countercurrent hydrochloric acid leaching process. The wet process steps include storage and filtration of the slurry after ore dressing, two-stage hydrochloric acid leaching under atmospheric pressure, washing and filtration of the silicon slag after leaching, removal of iron and nickel precipitation from the leaching solution, separation, washing and filtration of the obtained iron hydroxide and nickel hydroxide, crystallization and evaporation of the magnesium chloride solution, and production of hydrochloric acid using the gas generated after the thermal decomposition of magnesium chloride. The present invention has developed a serpentine decomposition technology using hydrochloric acid, a metallic magnesium production process using a drying-electrolytic method, and a process for producing industrial silicon by smelting silicon slag in an electric furnace.

The invention relates to the technical field of metal alkoxide preparation, and particularly provides a method for rapidly solidifying aluminum isopropoxide, which comprises the following steps: concentrating liquid aluminum isopropoxide in vacuum at 80-90 DEG C until the concentration is greater than or equal to 95%; sequentially adding 0.1 to 0.2 percent of a crystallization assisting solvent TXIB, 0.05 to 0.1 percent of a nanoscale aluminum isopropoxide seed crystal and 0.01 to 0.1 percent of a magnesium isopropoxide eutectic seed crystal; crystallization is completed through gradient cooling, and the whole process is less than or equal to 24 hours; and finally, carrying out solid-liquid separation, washing and drying to obtain the high-purity aluminum isopropoxide crystal. Through the synergistic effect of the bifunctional seed crystal and the TXIB, the crystallization period is remarkably shortened, the crystal quality is improved, and the method is suitable for industrial production.

The application discloses a preparation method of high-purity trans-4-propionylcyclohexylbenzene, and belongs to the technical field of liquid crystal material preparation. The method is based on dynamic synergy of three-stage gradient temperature control, seed addition in batches and intermittent stirring, and in a single petroleum ether solvent system, crystal growth is induced through ultralow-temperature cyclic crystallization and precise temperature control; in combination with a matching filter-drying integrated machine, continuous operation of low-temperature solid-liquid separation and vacuum drying is realized. The application significantly improves the purity and yield stability of the product, and one-time high-purity crystals are obtained, overcoming the problems of incomplete impurity separation, high energy consumption and large batch fluctuation in the traditional process, and simultaneously adapting to the industrial production demand, and providing a green and efficient high-purity preparation path for liquid crystal intermediates.

Disclosed is a preparation system and a preparation method for high-quality xylitol crystals. The preparation system comprises a blending tank, a heat exchanger, a decolorization tank, an ion exchange system, a microporous filter, a first evaporator, a first crystallization kettle, a first centrifuge, a fluidization drying bed, a xylitol dissolution tank, a second evaporator, a second crystallization kettle, a second centrifuge, a hot air drying tank, and a cold air fluidization bed sequentially connected through pipelines. Liquid outlet of the first centrifuge is connected with first inlet of the blending tank. Liquid outlet of the second centrifuge is connected with first inlet of the xylitol dissolution tank. The blending tank is provided with second inlet for receiving xylitol hydrogenation solution. The xylitol dissolution tank is provided with water inlet for pure water. The material output from a product outlet of the cold air fluidization bed is xylitol crystal product. First prepared xylitol crystals are redissolved and recrystallized to prepare xylitol crystals with higher pH and better flavor.

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.

A process for treating fluids for the removal of sulphate therefrom, the process comprising passing a fluid containing a sulphate and carbonate through a fluidized bed reactor; and, loading sulphate to said fluidized bed reactor at a rate that is greater than 1 kg of sulphate per square metre of said fluidized bed reactor per hour (kg SO4 / m2 / hr); thereby co-precipitating the sulphate and carbonate. The process must maintain the supersaturation levels of calcium sulphate within a predefined range of 100-450% and provides a loading rate of sulphate in the reactor that is greater than 1 kg of sulphate per square metre of reactor per hour (kg SO4 / m2 / hr).

The invention discloses a crystallization method of fructose and crystalline fructose prepared by the crystallization method, and belongs to the technical field of crystallization. The fructose crystallization method comprises the following steps: taking isomerized fructose syrup, adding glucose oxidase, catalase and calcium carbonate under stirring and ventilation until the pH value is stable, and carrying out plate frame filtration to obtain a feed liquid A; filtering the feed liquid A through a microbial flocculant, and removing impurities through a ceramic membrane, an ultrafiltration membrane and an electrodialysis system at a certain temperature and pressure to obtain feed liquid B; evaporating and concentrating the feed liquid B, adding a nucleating agent and a sugar molecule integrating agent while stirring, and cooling and crystallizing in stages to obtain feed liquid C; and centrifuging the feed liquid C, and carrying out vacuum microwave drying to obtain crystalline fructose. The method is high in extraction yield and purity, large in treatment capacity, high in continuous degree and suitable for large-scale industrial production.

The present invention relates to a method for producing high-purity arabinose crystals, which comprises sequential steps of dissolving, blending, ion exchange, decolorization filtration, microfiltration, evaporation concentration, crystallization, centrifugation, drying, etc. During the production of arabinose crystals, the pH of the material is controlled to 4.3-7.5 and the temperature to 70°C or lower, thereby avoiding a decrease in purity due to the promotion of conversion of arabinose to miscellaneous sugars at high temperatures, and improving the purity of the produced arabinose crystals.

An apparatus for carrying out continuous precipitation or chemical reaction involving solids is provided. The apparatus includes a plurality of serially connected chambers. One or more of the chambers includes a volume reducer for decreasing and increasing the volume of a chamber to produce a pulse of fluid to downstream chambers.