107results about "Counter-current extraction" patented technology

The invention discloses a liquid-liquid reactor based on hydrodynamic cavitation, and belongs to the field of liquid-liquid reaction of chemical production, medicine production, wastewater treatment and the like. The liquid-liquid reactor comprises a chamber A provided with a first top surface and a first bottom surface, the inner diameter of the first bottom surface is gradually reduced from top to bottom, and a first arc transition section is arranged between the first top surface and the first bottom surface; a tangential leading-in first liquid inlet pipe is arranged above the chamber A; the chamber B is a flat disc-shaped chamber; the chamber B is provided with a second top surface and a second bottom surface; the chamber B is provided with a second liquid inlet pipe which is tangentially guided in; a second arc transition section is arranged between the cavity A and the cavity B; a third arc transition section is arranged between the second top surface and the second bottom surface; a liquid outlet pipe is arranged in the center of the cavity A, and a Venturi tube structure is arranged in the liquid outlet pipe; a flow guide piece is arranged in the center of the cavity B; the outer diameter of the flow guide piece is gradually reduced from bottom to top; and the flow guide piece is provided with an end part which is inserted into the liquid outlet pipe. According to the ultrasonic cavitation device, the defects that ultrasonic cavitation equipment adopted in production at present is higher in energy consumption and smaller in equipment size amplification are overcome, and the cavitation equipment is changed from research to industrialization.

The invention relates to a nylon 6 polymerization production method capable of fully recycling extractable oligomers, and relates to the technical field of nylon 6 polymerization production processes, the nylon 6 polymerization production method comprises a nylon 6 polymerization section, a nylon 6 slice extraction section, a nylon 6 wet slice drying section, an extract evaporation and concentration section and an extractable oligomer cracking and recycling section; in an extractable oligomer cracking and recycling section, by adjusting process conditions such as temperature, pressure and water content of an oligomer extraction concentrated solution, deep cracking of extractable substances is realized, and all cracking products can be recycled into a polymerization section for recycling, so that rapid accumulation of cyclic dimers in polymers is inhibited, no residues are generated in the polymerization process, and the production cost is reduced. Accumulation of cyclic dimers in a system can be effectively slowed down, the service life of a polymerization reactor is prolonged, and the quality of polymer products is improved.

The invention provides a method for preparing high-purity hafnium tetrachloride by wet extraction and separation, which comprises the following steps: stirring and leaching hafnium alloy waste serving as a raw material by using HNO3 and HF mixed acid, then adding thioacetamide, adjusting the pH value to 4-5, stirring and filtering; compounding tributyl phosphate, trioctylphosphine oxide and sulfonated kerosene to obtain a composite extracting agent, and stirring and mixing to form a homogeneous organic phase; in a hydrochloric acid medium, controlling the volume ratio of an organic phase to a water phase to be (2.5-3.5): 1, carrying out three-stage counter-current extraction, and standing for phase splitting; the extracted organic phase passes through an adsorption column filled with iminodiacetic acid modified silica gel; and carrying out reverse extraction by using a hydrochloric acid solution, and then carrying out reduced pressure evaporation concentration, cooling crystallization and dehydration to obtain hafnium tetrachloride. According to the method, the zirconium and hafnium separation efficiency in the hafnium tetrachloride preparation process is improved, and the problem that the content of zirconium and hafnium impurities in the product is too high is solved.

The invention discloses a method for efficiently extracting phenol from coal tar and primarily separating crude phenol oil, and relates to the technical field of chemical separation. Carrying out multi-stage cross-flow or counter-flow extraction on the extracting agent and the coal tar to obtain a raffinate phase and a high-concentration extraction phase; and mixing the raffinate with condensate at the top of the regeneration device and supplemented fresh water, and recovering residual organic amine through a reverse extraction device to obtain a dephenolized oil product and backwashing water. Mixing and diluting the extract phase with backwashing water, and standing for phase splitting to obtain a high-grade crude phenol oil phase and a low-concentration extract phase; the low-concentration extraction phase absorbs CO2 in the industrial tail gas for acidification to obtain a low-grade crude phenol oil phase and an amine salt aqueous solution; and desorbing the amine salt aqueous solution to obtain a regenerated extraction agent (circularly used for extraction), tower top condensate (circularly used for reverse extraction) and water-containing industrial-grade CO2 gas (recycled or sealed after drying). According to the method, high-efficiency extraction of the phenolic compounds in the coal tar and primary separation of crude carbolic oil are realized by utilizing the extraction performance differences of extraction capacities, selectivity and the like of the extraction agents with different concentrations on the phenolic compounds, and the production economy is improved.

The invention relates to the technical field of bottled beverage production, in particular to a tea beverage efficient extraction production system which comprises a pre-treatment unit, a tea soup preparation unit and a waste heat recovery unit, the pre-treatment unit comprises a water tank, a hydraulic filter and an ion exchanger, and the hydraulic filter is provided with a water inlet and a water outlet; the tea soup preparation unit comprises a three-stage counter-current extraction tower, a standing tank and a cooling tower; the waste heat recovery unit comprises a steam condensation device and a heat energy storage tank, one end of the steam condensation device is communicated with the material inlet and outlet of the three-stage counter-current extraction tower, and the other end of the steam condensation device is externally connected with a CIP cleaning system. Through dynamic gradient temperature control extraction, a multi-stage counter-current extraction technology and an instantaneous cooling system, the production efficiency and the energy utilization rate are remarkably improved while the tea soup quality is guaranteed, and therefore efficient, energy-saving and intelligent tea beverage production is achieved.

The invention discloses a method and system for comprehensively utilizing a water phase in an aniline methylation reaction product, and the method comprises the following steps: firstly, taking the water phase in the aniline methylation reaction product as a raw material, and rectifying the raw material to obtain a methanol distillate and a mixed solution containing aniline, N-methylaniline, trace N, N-dimethylaniline organic matters and water; a low-boiling-point aromatic hydrocarbon solvent is used as an extraction agent, the obtained mixed solution is used as a raw material, and the raw material and the extraction agent are subjected to multiple times of reverse contact for extraction; standing and layering to obtain an extraction phase and a raffinate phase; wherein the extraction phase is a mixture of an amine organic matter and an extraction agent, and the raffinate phase contains wastewater with the content of the amine organic matter reduced. According to the method, the methanol, the amine mixed organic matters and the extraction agent can be recycled, the content of the organic matters in the water can be remarkably reduced, the water can be discharged after reaching the standard after being subjected to further biochemical treatment, and the resource comprehensive utilization of the water phase solution is realized.

The present invention relates to a column for the liquid-liquid extraction of a feedstock by an extraction solvent, comprising perforated trays (Pi) for the passage of a dispersed phase (B), the perforated trays being spaced apart by an inter-tray space (8), and comprising spillways (6), a spillway being a hole allowing the passage of a continuous phase (A) through a perforated tray, the extraction column (1) alternately comprising perforated trays of type I having two peripheral spillways, and perforated trays of type II having a single central spillway, wherein: the height H1 of the inter-tray spaces located directly downstream of the trays of type I, in the direction of flow of the continuous phase, is greater than the height H2 of the inter-tray spaces located directly downstream of the trays of type II. The present invention also relates to a liquid-liquid extraction method using said liquid-liquid extraction column.

A column for the liquid-liquid extraction of a feedstock by an extraction solvent, containing sieve trays (Pi) for a dispersed phase (B) to pass through, the sieve trays being spaced apart by an inter-tray space (8), and riser / downcomer conduits (6), a riser / downcomer conduit being an opening that allows a continuous phase (A) to pass through a sieve tray, the extraction column (1) containing, in alternation, type-I sieve trays containing two peripheral riser / downcomer conduits, and type-II sieve trays containing a single central riser / downcomer conduit, wherein: the height H1 of the inter-tray spaces situated directly downstream of the type-I trays, in the direction of flow of the continuous phase, is greater than the height H2 of the inter-tray spaces positioned directly downstream of the type-II trays. Also, a liquid-liquid extraction method that makes use of the liquid-liquid extraction column.

An extractor with a housing, conveyor assembly, and a plurality of recycle stages which are configured to direct a flow of solvent or miscella upwardly through a material bed.

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.

A countercurrent extraction device for spinning includes an extraction box containing extraction liquid, and the extraction box is provided with a plurality of partition assemblies, and the extraction box is partitioned into a plurality of extraction chambers by the partition assemblies; each of the partition assemblies includes a first plate and a second plate, two ends of the first plate are fixedly connected to two sidewalls of the extraction box, and a first gap is provided between a lower edge of the first plate and a bottom wall of the extraction box; a lower edge of the second plate is connected to the bottom wall of the extraction box, a second gap is provided between a top edge of the second plate and a top wall of the extraction box, and heights of a plurality of second plates are gradually decreased along a flow direction of the extraction liquid.

The invention discloses a method for recovering ammonium fluoride from semiconductor photovoltaic wastewater. The method comprises the following steps: adjusting pH in a pretreatment stage, and adding sodium citrate to complex metal ions; a composite extraction agent composed of diisooctyl phosphate, trialkyl phosphine oxide and methyl trioctyl ammonium chloride is adopted for multi-stage counter-current extraction; sequentially carrying out washing and two-stage gradient ammonia water reverse extraction to improve the selectivity and inhibit silicon-boron co-dissolution; the strip liquor is subjected to calcium and magnesium salt impurity removal, reduced pressure evaporation, graded cooling crystallization and vacuum drying, an ammonium fluoride product with the purity larger than or equal to 94% and the water content smaller than or equal to 0.5% is finally obtained, the extracting agent can be recycled, mother liquor and washing liquor are recycled, and the process is closed, environmentally friendly, economical and suitable for industrial application.

An extractor apparatus that incorporates an autoclave that defines an interior, which extends along a longitudinal axis between opposite media inlet and discharge ports. Also included is a feed assembly that is coupled to the inlet port to supply media during operation to the interior, which establishes a media bed movable about the longitudinal axis through the interior to the discharge port. Further incorporated is a solvent supply that is coupled to the autoclave proximate the discharge port to establish during operation pressurized solvent cross flow that is directionally opposite the direction of movement of movable bed. An extract port is also included, which is coupled to the autoclave proximate the inlet port to extract cross-flowed solvent from the movable media bed during operation. Further included is a capture assembly that is sealingly coupled to the discharge port and which during operation, captures spent media, and is movable to discharge the spent media. The capture assembly may also extract residual solvent from the spent media, which may be communicated to the interior between the inlet and discharge ports.

The invention relates to a column for the liquid-liquid extraction of a raw material by means of an extraction solvent, comprising: perforated trays (Pi) through which a dispersed phase (B) passes, the perforated trays being separated by inter-tray spaces (8); the invention relates to an extraction column (1) comprising a perforated tray (2) and comprising an overflow channel (6) which is a hole allowing a continuous phase (A) to pass through the perforated tray, the extraction column (1) alternately comprising a type I perforated tray with two peripheral overflow channels and a type II perforated tray with a single central overflow channel, the height H1 of the inter-tray space located directly downstream of the I-type tray is greater than the height H2 of the inter-tray space located directly downstream of the II-type tray. The invention also relates to a liquid-liquid extraction method using the liquid-liquid extraction tower.

The invention relates to the technical field of coffee bean treatment, in particular to low-caffeine treatment equipment and method by combining supercritical CO2 with molecular sieve directional adsorption, and the low-caffeine treatment equipment comprises an extraction kettle, and a fluid circulation mechanism and a treatment tank which are arranged on the left side and the right side of the extraction kettle, the extraction kettle comprises a kettle body which allows CO2 fluid to flow from bottom to top and is used for placing coffee beans, a filter cartridge arranged at the center in the kettle body, and an auger arranged in the filter cartridge. According to the invention, a dynamic circulating extraction structure of coffee beans is constructed by arranging the auger driven by the motor and the filter drum in the extraction kettle, and the coffee beans continuously rise in the filter drum under the lifting action of the auger and are uniformly scattered from the top end, and form countercurrent and dynamic full contact with supercritical CO2 which is introduced from the bottom of the kettle and flows upwards, so that the extraction efficiency of the coffee beans is improved. A traditional static soaking mode is changed, the contact area and updating frequency of coffee beans and a solvent are increased, the single-batch processing time is shortened, and the situation of local excessive extraction or insufficient extraction is avoided.

The invention relates to a column for the liquid-liquid extraction of a raw material by means of an extraction solvent, comprising: perforated trays (Pi) through which a dispersed phase (B) passes, the perforated trays being separated by inter-tray spaces (8); the invention relates to an extraction column (1) comprising a perforated tray (2) and comprising an overflow channel (6) which is a hole allowing a continuous phase (A) to pass through the perforated tray, the extraction column (1) alternately comprising a type I perforated tray with two peripheral overflow channels and a type II perforated tray with a single central overflow channel, in which: the central overflow channel has a cross-section S2 larger than the cross-section S1 of the peripheral overflow channels, and the cross-section S2 of the central overflow channel is larger than the cross-section S1 of the peripheral overflow channels; and the cross section S1 corresponds to the sum of the cross sections of the two peripheral overflow channels. The invention also relates to a liquid-liquid extraction method using the liquid-liquid extraction tower.

The invention belongs to the technical field of nitration reaction product separation, and particularly relates to a mixed dinitrobenzene extraction separation process applied to nitration reaction. Through three-section gradient dilution and accurate concentration control, the problem of incomplete separation caused by high solubility of high-concentration sulfuric acid to nitrobenzene is effectively solved, meanwhile, the hidden danger of pipeline blockage caused by dinitro compound crystallization is eliminated, and the production safety and the product purity are remarkably improved. According to the invention, a complete material closed-loop system is established, the extractant-nitrobenzene is directly reused for nitration reaction after deep dehydration and impurity removal, and the waste sulfuric acid is completely returned to a production system for recycling after being treated, so that the utilization rate of raw materials is greatly improved, and the discharge of waste acid is reduced. According to the method, key parameters such as temperature, concentration and flow are monitored in real time, so that the nitration reaction yield is stabilized at 97.2% or above, the operation cycle of the device is effectively prolonged, and reliable technical guarantee is provided for industrial production.

Process for recycling a loaded aromatic capture oil containing polycyclic aromatic hydrocarbons. The invention relates to a process for reprocessing a loaded aromatic capture oil (11) comprising an aromatic capture oil and one or more polycyclic aromatic hydrocarbons, the process being characterized in that it comprises a step of separating said polycyclic aromatic hydrocarbon from the aromatic capture oil, the separation step being carried out by supplying a counter-current continuous contactor (100) with the loaded aromatic capture oil and with supercritical carbon dioxide (23). Figure for the abstract: Fig. 1.

The invention relates to a process for treating a biocrude feedstock obtained from a hydrothermal liquefaction treatment to reduce the content of inorganic compounds, comprising: - a step of diluting the biocrude feedstock with a light organic diluent to obtain a diluted biocrude feedstock; - a step of washing the diluted biocrude feedstock with at least one aqueous solvent, followed by a step of backwashing with a counter-solvent comprising at least one hydrocarbon cut at a specific boiling point, in one or more countercurrent liquid-liquid extraction columns; - a raffinate fractionation step to obtain at least the biocrude feedstock depleted in inorganic compounds and a phase comprising the diluent.

To provide a method for counter-current liquid-liquid extraction in a sub-millimeter conduit.SOLUTION: The method is implemented from an initial liquid drop stream in a conduit. The initial liquid drop stream is constituted of alternating drops of a first liquid (LB) and a second liquid (LNM) less wetting than the first liquid and immiscible with the first liquid, one of the two liquids comprising a component to be extracted toward the other of the two liquids. The method comprises the steps of: (a) applying a first pressure gradient along the conduit to generate a visco-inertial flow displacing a first volume of drop stream according to a first gradient and generating a film of first liquid displaced along an opposite orientation to the first gradient (the film being located between the drops of second liquid and the conduit); (b) stopping the application of the first pressure gradient; (c) applying a second pressure gradient along the conduit, in the opposite orientation to the first pressure gradient applied to generate a viscous-capillary flow displacing a second volume of drop stream; and (d) stopping the application of the second pressure gradient.SELECTED DRAWING: Figure 3

One exemplary embodiment can be a process for oxidizing one or more thiol compounds from an alkaline stream. The process may include passing a mixed stream having the alkaline stream to a vessel having an oxidation section, a separation section and a vent gas section. Often, the oxidation section includes a body containing one or more packing elements. The process can further include passing an oxidized alkaline stream to the separation section containing a first chamber and a second chamber. Usually, the first chamber contains a coated mesh and packing. The two sections further form a neck contains a packing, a distributor, and a mesh.

A solvent extraction process may be used to generate a miscella stream. The miscella stream may be processed by a separation device, such as a decanter, to form a light phase stream and a heavy phase stream. In some examples, a portion or all of the light phase recycle stream passes to a solvent purification device, such as a membrane, that separates the feed stream into a purified solvent stream and a concentrated light phase stream. The purified solvent stream may be solvent that is substantially or completely free of oil. The concentrated light phase stream contains a portion of the solvent from the feed stream together with nearly all or all of the oil in the feed stream. The purified solvent stream can then be used to supplement the fresh solvent feed to the extractor.

The present invention provides a hydrodynamic-cavitation-based liquid-liquid reactor and a method thereof, and an apparatus. The reactor comprises a chamber A and a chamber B, wherein the chamber A is configured to convey a first fluid so as to make same rotatably enter a cavitation reaction unit in a central region; the chamber B is configured to convey a second fluid so as to make same rotatably enter the cavitation reaction unit to mix with the first fluid; and an axially adjustable flow guide member is provided in the central region to assist with drainage. The present invention achieves high-efficiency mass transfer of multiphase fluids in a controllable cavitation field by means of an innovative dual-tangential reverse feeding structure, adjustable flow guidance and Venturi coupling design, forming reaction intensification through swirling flow impingement, mixing and cavitation collapse; moreover, intelligent regulation and control of a reaction path is achieved by means of the micro-injection of gas and flow field adjustment, thus significantly improving the reaction rate, selectivity and energy efficiency ratio. Thus, the present invention has good engineering adaptability and prospects for large-scale application.

The invention relates to a system and a process for continuously preparing 3-(methylsulfonyl) propionic acid. The system comprises a feeding unit and a discharging unit, wherein the feeding unit comprises an acrylic acid continuous supply device, a sodium methyl mercaptide solution and sodium hydroxide solution mixed solution continuous supply device and an oxidizing agent continuous supply device; according to the system for continuously preparing the 3-(methylsulfonyl) propionic acid, provided by the invention, by using the continuous micro-channel reactor, rapid conversion and relatively high conversion rate of materials in addition reaction and oxidation reaction are realized; the safety of the oxidation reaction is effectively controlled, the liquid holdup is small, and the intrinsic safety of the oxidation reaction is reduced through the continuous reaction; by using the continuous extraction device, higher extraction efficiency is realized, the generation of three wastes is reduced, and higher yield is realized.

The invention relates to a method for separating a cyclohexane oxidation product, the purity of a cyclohexanol and cyclohexanone mixture obtained by the method is higher than 99%, the mass yield is higher than 95%, a caustic soda solution does not need to be added in the separation process, and three-waste discharge and environmental pollution are avoided; the stability of the circulating solvent is further improved, so that the device can operate for a long period.

Method for selectively extracting salts to be extracted from brine The present invention relates to a method for selectively extracting a salt to be extracted from a brine to be treated containing the salt, wherein the brine to be treated (S1) is sent to an initial extraction agitator-mixer (1a) in which a liquid hydrophobic organic phase is also introduced, the brine and the liquid hydrophobic organic phase are mixed in the initial extraction agitator-mixer (1a), and the mixture is sent to an initial decanter-separator (1d, 1dc) to obtain a brine freed of the salt to be extracted and an organic phase loaded with the salt to be extracted, and the brine freed of the salt to be extracted is recovered and used for extraction. The organic phase loaded with salts to be extracted is sent to an initial wash agitator-mixer-decanter-centrifuge (5a, 5dc or 7a, 7dc) to obtain a purified organic phase loaded with salts to be extracted, which is then sent to the so-called "organic" heat exchanger (1e) where it is heated before being sent to the so-called initial "regeneration" column (1c; 2c) where it undergoes countercurrent exchange with hot water at a temperature higher than that of the initial brine to obtain water containing the salts to be extracted and a regenerated organic phase depleted of the salts to be extracted, which is recycled to the initial extraction agitator-mixer (1a).

A dynamic cocurrent and countercurrent extraction device belongs to the technical field of extraction equipment and comprises a cocurrent extraction tank, a countercurrent extraction tank and a transition extraction tank, a first stirring shaft is arranged in the down-flow extraction tank, a spiral stirring propelling blade is arranged on the first stirring shaft, the outer end of the first stirring shaft is externally connected with a first stepping motor, and an extracting solution outlet is formed in the tank wall of the inner end of the down-flow extraction tank; a second stirring shaft is arranged in the countercurrent extraction tank, a spiral stirring push-out blade is arranged on the second stirring shaft, the outer end of the countercurrent extraction tank is externally connected with a second stepping motor, a slag outlet and a solvent injection port are formed in the tank wall of the outer end of the countercurrent extraction tank, and the transition extraction tank is communicated with the downstream extraction tank and the countercurrent extraction tank; the device has the beneficial effects that the flowing direction of a solvent is opposite to the entering direction of materials, so that the solvent is in full contact with medicinal materials, the extraction efficiency is improved, the extraction period is shortened, and the production efficiency is improved.

A hydrometallurgical process for the selective recovery of silver from a solid waste material, said solid waste material deriving from waste electrical and electronic equipment and / or from exhausted Ag-based catalysts, comprises the following steps: I) Subjecting said solid material to acid leaching to dissolve said silver by using a leaching solution, wherein said leaching solution is an aqueous solution of sulphuric acid, ferric sulphate and thiourea (H2SO4-Fe2(SO4)3-CH4N2S), said subjecting to acid leaching being carried out at ambient temperature and at atmospheric pressure, in a single stage or in multiple stages; filtering the exiting leaching solution and subjecting the residual solid material to washing with water; wherein said sulphuric acid, said ferric sulphate and said thiourea are contained in said leaching solution at the following concentrations: sulphuric acid 0.1-0.5 M; ferric sulphate 10-40 g / L; thiourea 10-40 g / L; II) Recovering said water used during said washing in said step I, replenishing said water with said sulphuric acid, said ferric sulphate and said thiourea and, when said subjecting to acid leaching is carried out in multiple stages, using said water as a leaching solution in said multiple stages, wherein said replenishing said water comprises adding said sulphuric acid, said ferric sulphate and said thiourea according to the following percentages compared to the dosage thereof in said step I: sulphuric acid 10-50%; ferric sulphate 80-100%; thiourea 25-50%; III) Subjecting said leaching solution exiting from said step I to electrolysis under stirring to recover said silver as metallic silver at the cathode and regenerate said thiourea; recovering said leaching solution at the end of said electrolysis; IV) Replenishing said leaching solution recovered at the end of said electrolysis in said step III con said sulphuric acid, said ferric sulphate and said thiourea, and, after said replenishing, reusing said leaching solution to treat a new solid waste material.

The invention relates to the technical field of tea leaf extraction, in particular to a dynamic countercurrent ultrasonic enhancement device for extracting functional components of tea leaves, which comprises a treatment tank, a cover plate is arranged on the treatment tank, a tea leaf pretreatment assembly is arranged on the cover plate, and the tea leaf pretreatment assembly comprises a lifting tank used for extracting the functional components of the tea leaves, the cover plate is arranged at the top end of the lifting tank and used for sealing, and a through hole is formed in the center of the cover plate. When a rotating motor drives a grinding sheet to rotate, tea leaves located at the top end of a filter plate can be ground and crushed, and in the grinding and crushing process, due to the fact that the tea leaves are stirred by the grinding sheet, the crushed tea leaves can fall into a screening tank through holes in the filter plate in the stirring process to be subjected to secondary screening; the problem that the tea leaves are directly extracted after being ground and crushed into different particle sizes, and the extraction effect is poor is avoided.