45results about "Fractional crystallization" patented technology

Producing high purity lithium solution from a source brine containing at least 1 mg Li / kg brine, preferably 10 mg / kg, more preferably 25 mg Li / kg brine; treating the source brine, if necessary in pretreatment steps; processing the treated brine in a lithium adsorption step; after the adsorption step, desorbing the adsorbed lithium in a desorption step; after the desorption step, treating the desorption effluent in an enrichment step. Specified optional steps and new features can be used to increase lithium concentrations and purity.

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 twice crystallization method for extracting hesperidin, and belongs to the technical field of plant extraction. The method for extracting hesperidin comprises the following steps: cleaning and crushing a raw material rich in hesperidin; adding an impurity removal solvent, and carrying out impurity removal reaction; adding an extraction solvent into the raw materials subjected to impurity removal to carry out extraction reaction, wherein the extraction solvent is a mixed solution of low-level saturated monohydric alcohol with the volume percent of 40-80% and alkali with the mass percent of 0.3-1.0%; adding acid into the extracting solution to adjust the pH value to 7.5-8.5; carrying out a first crystallization reaction, adding acid into the residual mother liquor to adjust the pH value to 6.5-7.5, and carrying out a second crystallization reaction; the extraction, purification and recovery processes of the hesperidin are optimized through a two-time crystallization method of sequentially performing crystallization in an alcohol system and a water system. The method not only overcomes the defects of large wastewater discharge amount and complex process of the traditional extraction process, but also further improves the extraction yield of hesperidin, reduces the production cost, and makes the extraction process more efficient and environment-friendly.

A method and system for separating sublimable compounds from hydrocarbons are disclosed. A feed fluid stream consisting of hydrocarbons and sublimable compounds is introduced into the upper chamber of a vessel. The feed fluid stream is cooled in the upper chamber, causing a portion of the sublimable compounds in the feed liquid stream to sublimate to form a product gas stream and a sublimable compound snow-like substance, the latter of which is collected in the lower chamber of the vessel. The lower portion of the sublimable compound snow-like substance is melted to form a liquid sublimable compound stream, such that the upper portion of the solid sublimable compound snow-like substance remains as an insulating barrier between the upper chamber and the liquid sublimable compound stream. The sublimable compound stream is removed from the ore liquid at a rate matching the rate of formation of the solid sublimable compound snow-like substance, thereby maintaining the insulating barrier.

The present disclosure relates to a method for isotopic separation of lithium, the method comprising:—providing a first mixture (104) comprising at least lithium, lithium hydride, and possibly lithium deuteride and / or lithium tritide, the first mixture being at a first temperature;—a first cooling step (110), preferably a uniform cooling, adapted to cooling the first mixture at a second temperature lower than the first temperature; the first cooling step being adapted to precipitating a first part of the lithium hydride having a first lithium isotope;—a first separation step (124) adapted to separating the precipitated first part of the lithium hydride from the first mixture, forming a second mixture (122).

The present disclosure relates to a method for separating lithium from a lithium mixture, the method comprising: —providing a first mixture (104) comprising lithium, lithium hydride, and at least a first compound among lithium deuteride and lithium tritide, the first mixture being at a first temperature: —a first stirring step (108) adapted to stirring the first mixture: —a first cooling step (110) adapted to cooling. preferably uniformly. the first mixture to a second temperature lower than the first temperature: the first stirring and cooling steps being adapted to deposit at least part of the first compound: and —a first separation step (116) adapted to separating at least the deposited first compound from the first mixture. forming a second mixture (118) comprising at least lithium and lithium hydride.

The present invention relates to a brine valorisation system for recovering at least one mineral salt and / or at least one metal from a monovalent brine (MVB) stream and / or a polyvalent brine (PVB) stream, the brine valorisation system comprising: I. (a) an ultra-high pressure reverse osmosis (UHPRO) system (402) for processing the MVB stream (104a) into a UHPRO retentate and desalinated water; (b) either (I) an osmotically assisted reverse osmosis (OARO) system (404) comprising one or more OARO stage or (ii) a thermal evaporation unit, for concentrating the UHPRO retentate to produce a concentrated UHPRO retentate; and (c) a crystallizer system (406) for processing at least a portion of the concentrated UHPRO retentate to produce distilled water, a monovalent purge stream and a mineral salt, wherein the mineral salt comprises sodium chloride crystals; and / or II. two or more clarifiers for processing the PVB stream, wherein the two or more clarifiers comprise a calcium clarifier and a magnesium clarifier, and wherein the calcium clarifier produces a calcium rich sludge comprising a calcium salt and / or metal, and a low calcium supernatant, and the magnesium clarifier produces a magnesium rich sludge comprising a magnesium salt and / or metal, and a low magnesium supernatant. Also provided is a system for recovering at least one mineral salt and / or at least one metal from seawater and / or another high salinity solution using the brine valorisation system of the invention; as well as methods for recovering at least one mineral salt and / or at least one metal from a monovalent brine (MVB) stream and / or a polyvalent brine (PVB) stream.

The object of the present invention is to provide a gradient cooling falling-film dynamic crystallizer and a falling-film crystallization separation method for mixtures in view of the problems existing in the existing dynamic crystallization devices, belonging to the technical field of chemical engineering equipment. The gradient cooling falling-film dynamic crystallizer of the present invention comprises, from top to bottom, a feeding unit, a falling-film crystallization unit and a discharging unit; the upper part of the feeding unit is a flow-smoothing tank and the lower part is a raw material tank; several falling-film tubes are arranged inside the falling-film crystallization unit, a jacket tube is sleeved on the outer wall of the falling-film tube, and a circulating water inlet and an outlet are arranged on the side wall; the base of the falling-film crystallization unit is fixedly connected to the top of the discharging unit, and a material outlet is arranged on the side wall of the lower part of the falling-film crystallization unit. The present invention solves the stability and uniformity of the material entering the dynamic crystallizer by setting a flow-smoothing tank; avoids the accumulation of crystallization scale in the initial stage by improving the uniformity of the material spraying on the inner wall of the falling-film tube; and improves the crystallization efficiency of the tube side by improving the heat exchange efficiency.

The invention relates to the technical field of lithium compound purification and crystallization, in particular to a lithium hydroxide solution multi-stage cooling crystallization device and a working method thereof.The lithium hydroxide solution multi-stage cooling crystallization device comprises a raw material liquid storage tank, a concentrator, a filter, a first-stage crystallizer, a second-stage crystallizer, a third-stage crystallizer, a centrifugal separator and a drying machine; the first-stage crystallizer, the second-stage crystallizer and the third-stage crystallizer are connected in series through a delivery pump, the third-stage crystallizer comprises a kettle body, a jacket is arranged in the kettle body, a feeding hole is formed in the top of the kettle body, and a discharging hole is formed in the bottom of the kettle body; by means of the unique design of the sealing cover, the discharging inner cavity and the built-in discharging channel, fine crystals scraped on the inner wall are collected and guided out of the kettle at the moment of generation. The problem of secondary pollution caused by a traditional wall scraping mechanism is thoroughly solved, secondary nucleation induced by fine grains is avoided from the source, and the method is the key for obtaining products with narrow particle size distribution.

The present invention relates to a brine valorisation system for recovering at least one mineral salt and / or at least one metal from a monovalent brine (MVB) stream and / or a polyvalent brine (PVB) stream, the brine valorisation system comprising: I. (a) an ultra-high pressure reverse osmosis (UHPRO) system (402) for processing the MVB stream (104a) into a UHPRO retentate and desalinated water; (b) either (I) an osmotically assisted reverse osmosis (OARO) system (404) comprising one or more OARO stage or (ii) a thermal evaporation unit, for concentrating the UHPRO retentate to produce a concentrated UHPRO retentate; and (c) a crystallizer system (406) for processing at least a portion of the concentrated UHPRO retentate to produce distilled water, a monovalent purge stream and a mineral salt, wherein the mineral salt comprises sodium chloride crystals; and / or II. two or more clarifiers for processing the PVB stream, wherein the two or more clarifiers comprise a calcium clarifier and a magnesium clarifier, and wherein the calcium clarifier produces a calcium rich sludge comprising a calcium salt and / or metal, and a low calcium supernatant, and the magnesium clarifier produces a magnesium rich sludge comprising a magnesium salt and / or metal, and a low magnesium supernatant. Also provided is a system for recovering at least one mineral salt and / or at least one metal from seawater and / or another high salinity solution using the brine valorisation system of the invention; as well as methods for recovering at least one mineral salt and / or at least one metal from a monovalent brine (MVB) stream and / or a polyvalent brine (PVB) stream.

The present disclosure relates to a method for separating lithium from a lithium mixture, the method comprising the steps of providing a first mixture (104) comprising at least a first compound of lithium, lithium hydride, and lithium deuterium and lithium tritide and at a first temperature, a first stirring step (108) adapted to stir the first mixture, a first cooling step (110) adapted to cool the first mixture, preferably uniformly, to a second temperature lower than the first temperature, the first stirring step and the first cooling step adapted to deposit at least a portion of the first compounds, and a first separation step (116) adapted to separate at least the deposited first compounds from the first mixture and form a second mixture (118) comprising at least lithium and lithium hydride.

Disclosed herein are electro-dialytic crystallizers and methods of use thereof. For example, described herein are electro-dialytic crystallizer systems comprising an electro-dialysis module and a crystallizer module in liquid communication with the electrodialysis module. The electrodialysis module is configured to receive an aqueous feedwater solution and form a diluate stream and a brine stream, the aqueous feedwater solution comprising an ionic component, the diluate stream having a lower concentration of the ionic component relative to the aqueous feedwater solution, and the brine stream having a higher concentration of the ionic component relative to the aqueous feedwater solution. The crystallizer module is configured to receive the brine stream and form crystals comprising the ionic component and a supernatant. Also disclosed herein are methods of use of any of the systems disclosed herein, for example using the system to treat the aqueous feedwater solution.WO

Continuous process for the dry fractionation of edible oils and fats using one or more crystallizers connected in series, which process comprises the following steps: a) providing a melted fat; b) continuously feeding the molten oil or fat into the first of one or more series-connected crystallisers in which the fat is gradually cooled using heat exchangers containing a cooling medium to form a crystal slurry, each of the one or more crystallisers having a temperature gradient such that the temperature at the point at which the molten or partially crystallised fat enters one of the crystallisers is higher than that at the point at which the slurry leaves the crystalliser; c) continuously removing the slurry from the last of said one or more crystallizers; d) separating the crystal slurry by filtration into a filter cake and a filtrate; the process further comprising the step of at least partially melting grease deposits deposited on the heat exchangers.

The present invention describes a method to produce high purity hydrocarbon materials and the high purity hydrocarbon materials produced from renewable sources. The produced materials are chemically similar and of equal or higher purity to from highly refined mineral oils and / or synthetic hydrocarbons. These renewable hydrocarbon materials can be used as a replacement for mineral and synthetic hydrocarbon base oils, process fluids, white oils in products such as lubricants, rubber, personal care, pharma.

The present invention relates to a nitrogen closed-loop acetic acid recovery and flash drying system capable of continuous production. The system comprises a nitrogen source, a heater, an explosion-proof blower, a flash dryer, a screw feeder, a cyclone separator, a heat exchanger, a condenser cooler, a solvent recovery tank, and a first cryogenic crystallizer and a second cryogenic crystallizer arranged in parallel. Fins are provided in the first cryogenic crystallizer and the second cryogenic crystallizer, and a cold source medium for condensation and a hot source medium for liquefaction can be introduced into the fins. The first cryogenic crystallizer and the second cryogenic crystallizer can be alternately in a condensation and crystallization state and a heating and melting state, thereby realizing continuous recovery of acetic acid.

Provided is a method for stably obtaining a product. The present invention relates to a purification apparatus for purifying a compound, the purification apparatus including: a tank for use in the purification apparatus; and a hydraulic wash column, the tank being at least one of a crystallization tank that forms a slurry containing crystals of a compound or a ripening tank that is capable of keeping crystals of a compound suspended in the ripening tank, the tank including an agitator having an agitator shaft and a bearing, the purification apparatus further including: a line for discharging the slurry containing crystals of a compound from the tank and feeding the slurry to the hydraulic wash column; and a line for flowing between the agitator shaft and the bearing in the tank at least one of a mother liquor derived from the slurry fed to the hydraulic wash column, the slurry containing crystals of a compound, or a melt obtained by melting the crystals.

In the BHET crystallization process, the BHET solution is introduced into a crystallizer located at the bottom of the crystallizer and equipped with agitator blades arranged coaxially with the draft tube. The draft tube is arranged coaxially with the inner wall of the tank, and multiple heat exchange plates, through which a cooling fluid circulates, are placed in the gap formed between the inner wall of the tank and the draft tube. The thrust of the agitator blades drives the solution through the gap, and the large heat exchange area with the heat exchange plates allows for efficient cooling without excessive agitation of the liquid. The resulting suspension is rich in BHET crystals and low in fines, and is discharged from the crystallizer and sent to the subsequent BHET processing step.

A method for preparing a purified styrene composition includes providing a crude hydrocarbon composition containing styrene, subjecting the crude hydrocarbon composition to a distillation in a divided-wall column to produce an overhead hydrocarbon stream, a bottom hydrocarbon stream and a side hydrocarbon stream and subjecting the side hydrocarbon stream to at least one crystallization step to obtain a purified styrene composition.

The invention discloses a vacuum system condensate distribution device and an application method thereof, relates to a chemical production vacuum system condensate distribution technology, and aims to reasonably distribute the condensate of a vacuum system on the premise of ensuring the water balance of a circulating system and reduce the starting, stopping and operating cost of the device. According to the technical scheme, a stop valve is additionally arranged on an original process circulating water tank removal pipeline for condensate of a first condenser of an OAT crystallizer vacuum system, two pipelines for removing a flushing water tank and a process condensate tank and corresponding stop valves are additionally arranged, the condensate is cut into the flushing water tank in the starting and normal period, the water amount is absorbed by an ammonia absorption tower, and water balance is adjusted; during shutdown, condensate is cut into a process condensate tank and sent to a desorption device for treatment, system wastewater treatment is accelerated, the running time of a circulating system is shortened, and the shutdown cost is reduced.

A process for dry fractionation of a soft palm oil mid fraction (SPMF) into a final hard palm oil mid fraction (fHPMF-A)is disclosed. The process comprises: providing the soft palm oil mid fraction (SPMF), using the soft palm oil mid fraction (SPMF) as an input (IN1) to a first dry fractionation (FDF) to obtain an intermediate olein fraction (SPMF-O) and an intermediate stearin fraction (SPMF-S), using the intermediate olein fraction (SPMF-O) as an input (IN2) to an ultrasound assisted second dry fractionation (SDF) to obtain the final hard palm oil mid fraction (fHPMF-A) and a palm oil olein fraction (POO), wherein the ultrasound assisted second dry fractionation (SDF) comprises subjecting at least a part of the input (IN2) to ultrasonic treatment (US2). Also disclosed is afinal hard palm oil mid fraction (fHPMF-A), a second hard palm oil mid fraction (sHPMF-B), a hard palm oil mid fraction mixture, and uses of these.

The invention provides a device and a method for controlling gradient crystallization by a gas-liquid microreactor with a flow field structure, which are characterized in that the device comprises a gas storage bottle and is characterized in that the gas storage bottle is connected with a preheater through a gas outlet pipe, the preheater is connected with a microreactor through a gas conveying pipe, the top of the microreactor is connected with a gas-liquid separator through a pipeline, and the gas-liquid separator is connected with the gas-liquid separator through a pipeline. The bottom of the gas-liquid separator is connected with a crystal separation tank through a pipeline, the crystal separation tank is connected with a raw material liquid storage tank through a pipeline, a stirring mechanism is mounted in the raw material liquid storage tank, and the bottom of the raw material liquid storage tank is connected to the bottom of the microreactor through a pipeline; the gas-liquid micro-reactor is a vertical segmented micro-channel and is divided into three functional areas, namely a preheating section, a crystallization section and a curing section, and the sections are hermetically connected through flanges, so that the gas-liquid micro-reactor is convenient to clean and replace; the flow guide plates are spirally and obliquely arranged in the crystallization section, so that a bubble rising path can be disturbed, the gas-liquid contact time is prolonged, and the coupling effect of a flow field and a temperature gradient is enhanced.

The present invention relates to a method for treating salt-containing dusts which accumulate during operation of industrial plants, e.g. in waste incineration plants, or during operation of rotary kilns, e.g. in cement production plants or clinker production plants. The method comprises a step a) of forming an aqueous solution by bringing salt-containing dusts into contact with an aqueous phase; a step b) of removing heavy metals from the aqueous solution; and a step c) of separating alkali metal chlorides from the aqueous solution; and the bringing of salt-containing dusts into contact with an aqueous phase in step a) is achieved by means of a multi-stage arrangement through which the salt-containing dusts and the aqueous phase pass in opposite directions.

Provided is a method for purifying a compound capable of providing a high purity compound in high yield and at low cost. The present invention relates to the method for purifying a compound using a purification apparatus, the purification apparatus including: a crystallizing unit including a crystal forming section; and a wash column including a mechanism that forcibly transfers crystals. The crystallizing unit includes N tanks connected in series, wherein N is 2 or greater, a 1st tank is a most downstream tank, a (N)th tank is a most upstream tank, at least the 1st tank is a crystallization tank including a cooling mechanism, and a 2nd and subsequent tanks are each a crystallization tank or a ripening tank. The purification apparatus includes a line that feeds a compound-containing liquid to be purified to at least one of the N tanks. The wash column includes a line that sends a product out; and a line that returns a mother liquor to the crystallizing unit, with the line that returns a mother liquor to the crystallizing unit being connected to at least the (N)th tank. The crystallizing unit includes a line that feeds a slurry from the (N)th tank to the wash column; a line that sends a slurry from a tank among the 1st to (N - 1)th tanks to the next upstream tank; and a line that is provided to each of the 1st to (N - 1)th tanks and that sends thereto a mother liquor withdrawn from an upstream tank, wherein at least one of the lines that send a slurry from a tank among the 1st to (N - 1)th tanks to the next upstream tank is a line that sends a slurry from a tank to the next upstream tank via a solid-liquid separator and that has a line that returns a mother liquor from which crystals are removed in the solid-liquid separator to the tank where the slurry came from, and wherein the line that is provided to each of the 1st to (N - 1)th tanks and that sends thereto a mother liquor withdrawn from an upstream tank is a line that directly sends a mother liquor withdrawn from a tank one upstream or a line that sends a mother liquor withdrawn from a tank one upstream via a solid-liquid separator. The purification method includes forming crystals of the compound in the crystallizing unit; discharging at least a portion of a mother liquor to the outside of the purification apparatus; separating a slurry containing the formed crystals into a mother liquor and a slurry having an increased crystal concentration; returning at least a portion of the separated mother liquor to the tank where the slurry came from; mixing a compound-containing liquid to be purified fed to the crystallizing unit with a slurry in the crystallizing unit; sending a slurry in order from any one of the 1st to (N - 1)th tanks to the next upstream tank among the N tanks in the crystallizing unit; and feeding at least a portion of a slurry from the crystallizing unit to the wash column; wherein the compound-containing liquid to be purified has a higher purity than the mother liquor discharged to the outside of the purification apparatus, the slurry fed to the wash column contains a mother liquor having a purity A1 of 80 mol% or higher, and a difference between the purity A1 and a purity A2 of the mother liquor discharged, A1 - A2, is 5 mol% or more.

The invention relates to the technical field of ammonium sulfate evaporative crystallization, in particular to a continuous crystallization process and equipment for large-particle ammonium sulfate, and the equipment comprises an MVR evaporative crystallization unit, an evaporation-cooling coupling crystallization unit and a solid-liquid separation-retreatment unit; the MVR evaporative crystallization unit comprises a vapor compressor, an ammonia gas absorption tower, an evaporation chamber, a fine grain culture chamber, a first forced circulation heat exchange pump, a first heat exchanger and a fine grain extraction pump; the evaporation-cooling coupling crystallization unit comprises a flash chamber, a large-particle crystal raising chamber, a second forced circulation heat exchange pump, a second heat exchanger, a fine crystal circulating pump and a large-particle extraction pump; an ammonium sulfate solution is subjected to fractional crystallization through the MVR evaporative crystallization unit and the evaporation-cooling coupling crystallization unit, the MVR evaporative crystallization unit firstly performs primary crystallization on an ammonium sulfate raw material, then fine crystals are conveyed to the evaporation-cooling coupling crystallization unit for secondary crystallization, and the generated crystals are uniform in particle size distribution and uniform in particle size distribution. And continuous production of large-particle ammonium sulfate crystals is realized.

The present invention relates to a method for separating enantiomer crystals by enantioselective crystal flotation, and to a method in which preferential crystallization is combined with enantioselective crystal flotation.

Crystallization process of BHET in which a BHET solution is introduced into a crystallizer equipped with an impeller positioned in the lower part of the crystallizer and coaxial to a draft tube, which in turn is coaxial to the internal wall of the tank, which defines an interspace within which a plurality of heat exchange plates are placed in which a cooling fluid circulates. Thanks to the thrust of the impeller, the solution flows inside the interspace where the solution is cooled with high efficiency, thanks to the high exchange surface with the heat exchange plates, without generating excessive turbulence of the liquid. A suspension rich in BHET crystals with a low content of fines is therefore formed, which is then discharged from the crystalliser and sent to the subsequent BHET processing steps.

The present invention relates to a method for treating salt-containing dusts which accumulate during operation of industrial plants, e.g. in waste incineration plants, or during operation of rotary kilns, e.g. in cement production plants or clinker production plants. The method comprises: a step a) of forming an aqueous solution by bringing salt-containing dusts into contact with an aqueous phase; a step b) of removing heavy metals from the aqueous solution; and a step c) of separating alkali metal chlorides from the aqueous solution; and salt-containing dusts are brought into contact with an aqueous solution in step a) by means of a multi-stage arrangement through which the salt-containing dusts and the aqueous phase pass in opposite directions.

The invention relates to the technical field of separation equipment, and discloses continuous separation equipment and method for dipentaerythritol and tripentaerythritol sticky materials, the continuous separation equipment comprises a treatment cylinder which is used as a basic component of the whole device and is used for assembling and bearing all treatment mechanisms and subordinate lower structural components; and the front-end treatment mechanism is arranged in the treatment barrel and used for carrying out front-end separation treatment on solid impurities in the sticky materials. Through a running fit mode, the resistance of high-viscosity mother liquor to solid-liquid separation is ingeniously overcome, efficient dynamic separation of crystals and the mother liquor is achieved, under the action of a centrifugal force field, the viscous resistance of the high-viscosity mother liquor is effectively eliminated, dipentaerythritol crystals and tripentaerythritol crystals are rapidly settled and separated, and the separation efficiency of the crystals is improved. The problem of incomplete crystal entrainment and separation caused by overhigh mother liquor viscosity in traditional separation equipment is avoided, the liquid content of the separated wet crystals is remarkably reduced, and the energy consumption requirement of the subsequent drying process is greatly reduced.

The present invention relates to a process for the separation of enantiomeric crystals by enantioselective crystal floatation and to a process in which preferential crystallization is combined with enantioselective crystal floatation.

The invention relates to a method for crystallizing BHET, in which a BHET solution is introduced into a crystallizer equipped with an impeller which is located at the lower part of the crystallizer and is coaxial with a flow guide tube which is in turn coaxial with the inner wall of the tank, said inner wall defining a gap in which a plurality of heat exchange plates are placed, cooling fluid circulates in the heat exchange plates. Due to the thrust of the impeller, the solution flows in the gap, in the gap, the solution is efficiently cooled due to the high exchange surface of the heat exchange plate, and excessive turbulence of the solution cannot be generated. A suspension rich in BHET crystals and low in fines content is thus formed, which is then discharged from the crystallizer and fed to a subsequent BHET processing step.