240results about "Crystallization plant arrangements" patented technology

The invention provides an ultrasonic-assisted gamma-aminobutyric acid crystallization particle size regulation and control method, which comprises the following steps: removing impurities and decolorizing gamma-aminobutyric acid-containing feed liquid, heating, stirring and concentrating to a nearly saturated state, then carrying out ultrasonic-assisted crystallization, cooling, aging and suction filtration to obtain coarse crystals, and finally washing and drying to obtain target crystals. According to the method, a synergistic process of raw material liquid pretreatment, evaporation concentration-ultrasonic-cooling coupling crystallization, aging and post-treatment is adopted, an ultrasonic cavitation effect is utilized to reduce a nucleation barrier, and a supersaturation degree precise control and gradient cooling strategy is combined, so that grain size refinement, obvious narrowing of distribution and effective inhibition of agglomeration of crystals are realized; the median particle size of the crystal can be controlled to be smaller than or equal to 200 microns, the particle size distribution span is smaller than or equal to 1.5, the agglomeration phenomenon is remarkably inhibited, the crystal form is kept stable, the crystal habit is complete and smooth, the crystal product quality and the process efficiency are remarkably improved, and the method has important industrial application value.

The invention belongs to the technical field of coal chemical industry grey water treatment, and particularly relates to an advanced treatment method and system for coal chemical industry grey water circulating water. The method integrates pretreatment, complexing cracking, fractional crystallization and deep deamination, and is characterized in that a chelating structure of an organic phosphorus dispersing agent and calcium and magnesium ions is thoroughly destroyed through an advanced reduction-advanced oxidation combined process, target ions are released, and the core problems that hardness removal is hindered and phosphorus pollution is caused are solved; then, calcium and magnesium are respectively converted into calcium carbonate and magnesium ammonium phosphate particles for resource recovery by utilizing a secondary crystallization technology, so that the bottlenecks of high alkali liquor consumption and salt accumulation of a traditional high-pH magnesium ion precipitation method are broken through; and finally, the residual ammonia nitrogen is deeply removed by adopting a pollution-resistant PTFE hydrophobic membrane, so that the residual ammonia nitrogen is efficiently and stably removed, and the problem that a traditional polypropylene material membrane system is easy to pollute and block, easy to oxidize and difficult to apply to the field is solved.

The cooling crystallization production system comprises a crystallization unit, a product storage tank, a pipeline and a switching unit, the crystallization unit is composed of at least two parallel crystallizers, feeding ports of the crystallizers are connected with a discharging port of a distribution tank, and a discharging port of the distribution tank is connected with a discharging port of the product storage tank. Each crystallizer is a double-pipe heat exchanger, the shell pass of each crystallizer is a material flow path, and the tube pass of each crystallizer is a cold / hot medium flow path; the pipeline and switching unit is configured to selectively enable any crystallizer to be connected into a circulation loop, and in the circulation loop, materials circularly flow in the shell pass of the crystallizer through a circulation pump so as to achieve cooling crystallization. The crystallizer completing crystallization can be selectively switched to a discharging pipeline, and a heating medium is introduced into the tube pass of the crystallizer to melt crystals and then output the crystals into the product storage tank; compared with the prior art, a semi-continuous production mode is constructed, and the production cycle of unit products is shortened.

The invention discloses a crystallization device for sodium sarcosinate production, relates to the technical field of crystallization devices, and aims to solve the problems that when supersaturated liquid drops make contact with the wall surface of a low-temperature gas-liquid separator, water evaporation is intensified, the solubility of solute is further reduced due to temperature reduction, crystal precipitation is accelerated under the dual action, the supersaturated liquid drops are prone to being attached to the wall of a tank in the crystallization process, and the crystallization effect is poor. In order to solve the problems that the heat exchange efficiency is influenced by scaling of a tank wall, wall-adhered crystals cannot be recycled and the yield is reduced in the prior art, an evaporator is mounted on one side of a gas-liquid separator, a cyclone separator is mounted on the other side of the gas-liquid separator, an ultrasonic disperser is mounted on one side of the cyclone separator, a membrane filter is mounted on one side of the ultrasonic disperser, and a water outlet is formed in the other side of the membrane filter. A gas-liquid separator cleaning mechanism is mounted in the gas-liquid separator, a gas-liquid separator scraping frame is mounted at one end of the gas-liquid separator cleaning mechanism, and a membrane filter cleaning mechanism is mounted in the membrane filter.

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

To provide a process for forming drug crystals of narrow size distribution and desire dimensions and morphology.SOLUTION: The present invention relates to a process for providing corticosteroid crystals of desired size distribution and morphology, the process comprising the steps of: providing recrystallized ultra-large columnar crystals having aspect ratios of more than 1 and less than 20, the aspect ratio of a given columnar crystal being the ratio of a longest dimension along a lengthwise axis relative to a shortest dimension of a transverse plane perpendicular to the lengthwise axis; and sizing the recrystallized ultra-large columnar crystals to provide a collection of sized crystals having target dimensions, wherein the sizing includes segmenting at least a part of the recrystallized ultra-large columnar crystals along the respective lengthwise axes while retaining the dimensions of the transverse plane perpendicular to the lengthwise axis.SELECTED DRAWING: None

A process for production of both purified recycled aromatic dicarboxylic acid (rCA) and purified aromatic dicarboxylic acid (vCA), said process comprising:Producing a first stream comprising a recycled aromatic dicarboxylic acid by a first process, wherein the first process comprises the depolymerisation of a polymer feedstock comprising a polymer of said aromatic dicarboxylic acid in a first reaction system;Producing a second stream comprising the aromatic dicarboxylic acid by a second process wherein the second process comprises the oxidation of an aromatic hydrocarbon in a second reaction system;Purifying both the first stream and the second stream in a common purification system to thereby produce both purified recycled aromatic dicarboxylic acid (rCA) and purified aromatic dicarboxylic acid (vCA).The present invention also provides an apparatus for the production of both purified recycled aromatic dicarboxylic acid (rCA) and purified aromatic dicarboxylic acid (vCA),

It is provided an environmentally friendly process for recycling metals and nonmetallic components from printed circuit boards (PCBs), without using treatments considered damaging to the environment and minimizing emission of greenhouse gases comprising the steps of shredding the PCBs, micronizing the shredded PCBs producing a micronized powder, removing plastic and epoxy from the micronized powder, leaching, precipitating and recuperating the Al, Fe, Zn, Ni, Cr, Cu, Au, Ag, and Pd from the micronized powder, producing a filtrate from which the Cu is recovered. The solid product of the process is a concentrate of precious metals.

The application discloses a preparation method of polyaluminum chloride, and is characterized by comprising the following steps: S1, adding aluminum ash and hydrochloric acid solution into an acidification reaction tank, heating and reacting, filtering after the reaction is completed, and passing the filtrate into a polymerization reaction kettle; S2, adding calcium carbonate into the polymerization reaction kettle in batches to carry out polymerization reaction, stopping the reaction after the calcium carbonate is completely dissolved and the PH of the solution is 3-5; S3, adding polyacrylamide and ferric chloride into the polymerization reaction kettle, and precipitating under 1-3 pa low pressure to obtain sludge and upper liquid, concentrating and crystallizing the upper liquid, crushing the crystal, and obtaining polyaluminum chloride. The application increases an automatic blocking mechanism below a crystallization and crushing tank, automatically blocks when the sub-packaging cylinder is filled with crystals, achieves the purpose of quantitative sub-packaging, and does not cause too much or too little crystals in the sub-packaging cylinder, and does not require staff to be always beside the machine.

A recovery system for preparing magnesium sulfate using sulfuric acid waste liquid is provided. [Solution] The recovery system for preparing magnesium sulfate using sulfuric acid waste liquor according to the present invention comprises a reactor 1, a crystallizer 3, a dehydrator 4, and a dryer 5. The reactor 1 removes hydrogen peroxide from the sulfuric acid waste liquor and produces a magnesium sulfate solution. The crystallizer 3 continuously recrystallizes the magnesium sulfate solution by lowering its temperature, obtaining magnesium sulfate crystals and their mother liquor. The dehydrator 4 removes the mother liquor, and the dryer 5 dries the solution at different temperatures to obtain magnesium sulfate hydrates containing different amounts of water of crystallization.

The application discloses a cooling crystallization device for arsenic leaching solution, which comprises a cooling crystallization tank with a corresponding heat exchange jacket arranged on the periphery, a stirring mechanism comprising a hollow rotating shaft, the middle part of the hollow rotating shaft is connected with corresponding arc-shaped stirring plates through a plurality of material collecting pipes, a crystallization material discharging mechanism comprising a discharging one-way valve installed at the bottom of the hollow rotating shaft, a corresponding blocking push plate is installed in the hollow rotating shaft on the upper side of the material collecting pipe and can be lifted, the blocking push plate is rotationally connected to the end of the piston rod of a corresponding lifting drive oil cylinder through a corresponding connecting shaft, at least one liquid discharging one-way valve for discharging liquid material is installed on the blocking push plate, a corresponding filter screen plate is fixedly connected to the bottom side of the liquid discharging one-way valve, and the opening pressure of the liquid discharging one-way valve is smaller than that of the discharging one-way valve. The application can effectively separate the solid and liquid of part of the crystallized material, and can timely output the crystallization material after the solid-liquid separation.

The invention discloses a hydrolysate deacidification-dehydration coupling process and a byproduct recovery method, and belongs to the technical field of hydrolysate treatment. The method comprises the following steps: pretreating a hydrolysate raw material through two-stage filtration; adding the pretreated hydrolysate, a deacidification agent and a dehydration auxiliary agent into a coupling reaction device, and synchronously carrying out deacidification-dehydration reaction under the conditions of 60-120 DEG C and 0.1-0.5 MPa; after the reaction, separating to obtain a deacidification and dehydration product and a mixed solid phase; and dissolving and crystallizing the mixed solid phase to recover high-purity byproducts. The deacidification and dehydration synergistic interaction is achieved, the acidity reduction rate is larger than or equal to 85%, the water content is smaller than or equal to 5%, and the process time consumption is shortened by 28.6%; the byproduct purity is not less than 90%, and the recovery rate is not less than 80 A tail gas treatment system is additionally arranged to ensure that environmental protection reaches the standard. The process is suitable for biomass, polysaccharide and protein hydrolysate treatment, has the advantages of high efficiency, good resource utilization rate and the like, and provides an efficient solution for hydrolysate industrial treatment.

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.

A hybrid process and system for separating water from an inlet brine solution is disclosed. The hybrid process couples at least two different separation processes / systems. The inlet brine solution is fed into a first separation process, which produces a water distillate and a brine concentrate. The brine concentrate from the first separation process is then fed into the second separation process to further recover additional water. The excess heat from the second separation process is supplied to the first separation process.

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.

A method for producing mixed metal salts containing manganese ions and at least one of cobalt ions and nickel ions, the method including: an Al removal step of subjecting an acidic solution containing at least manganese ions and aluminum ions, and at least one of cobalt ions and nickel ions, to removal of the aluminum ions by extracting the aluminum ions into a solvent, the acidic solution being obtained by subjecting battery powder of lithium ion batteries to a leaching step; and a precipitation step of neutralizing an extracted residual liquid obtained in the Al removal step under conditions where a pH is less than 10.0, to precipitate mixed metal salts comprising a metal salt of manganese and a metal salt of at least one of cobalt and nickel.

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

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

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

A production system, production method and application of general-purpose high-purity chemicals are disclosed. The production system includes a raw material tank, and an adsorption system, a crystallizer, a first light-impurity removal tower, a first heavy-impurity removal tower, a second light-impurity removal tower, a motorized tower, a second heavy-impurity removal tower, a vapor permeation device, a membrane separation system and a filling system connected with the raw material tank in sequence. The high-purity chemicals produced by the above system have high purity and excellent quality. Compared with the prior art, the system and method designed by the present disclosure have more pertinence, integrity, progressiveness, energy-saving, precision, high safety coefficient and great industrial promotion value. And the products produced are of excellent quality, which can meet the standards applied to the manufacturing of integrated circuit electronic components and meet the high-end needs of the semiconductor industry market.

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

Methods and systems for the extraction of magnetic material from magnet containing material, and for extraction of rare earth elements (REEs) from the magnetic material are disclosed. An exemplary system includes a milling / washing unit for magnet containing material such as end-of-life motors, hard drives, partially deconstructed motors, magnet-containing end-of-life product, or parts thereof, and outputting magnetic components by exploiting magnetic properties of ferromagnetic and paramagnetic materials in the presence and absence of electromagnetic fields in conjunction with other physical properties such as size and density. The system also includes a chemical processing unit for receiving the magnetic components to extract rare earth elements in the material. Chemical processes are disclosed for separating rare earth elements from magnetic components.

In the crystallization system of the lithium hexafluorophosphate of the present invention, a first-stage crystallization kettle is connected to a lithium hexafluorophosphate mother liquor supply source through a lithium hexafluorophosphate mother liquor supply line; further connected to the lithium hexafluorophosphate mother liquor supply source through a mother liquor heat exchange line connected with a mother liquor heat exchanger; and further connected to a second-stage crystallization kettle through a first mother liquor delivery line configured to deliver lithium hexafluorophosphate mother liquor, a second-stage crystallization kettle is connected to a third-stage crystallization kettle through a second mother liquor delivery line configured to deliver lithium hexafluorophosphate mother liquor, a third-stage crystallization kettle is connected to a fourth-stage crystallization kettle through a crystalline particle delivery line configured to deliver small crystalline particles in the third-stage crystallization kettle; and further connected to a next process device through a first discharging line, and a fourth-stage crystallization kettle is connected to a next process device through a second discharging line. The crystallization system of lithium hexafluorophosphate of the present invention enables different crystallization stages to be carried out separately in different crystallization kettles, so as to realize continuous feeding and continuous discharging in the course of crystallization.

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

Described herein are methods of recovering lithium from dilute lithium sources. The methods include extracting lithium from an extraction feed using direct lithium extraction in an extraction stage to yield a lithium intermediate, performing one or more concentration operations, each concentration operation concentrating an input stream to yield an output feed, wherein the input stream is obtained from the lithium intermediate and / or the extraction feed is obtained from the output feed. At least one of the concentration operations includes a membrane separation operation having a plurality of reactors in series each having a semi-permeable membrane, such as a counter-flow reverse osmosis operation. Methods may also include generating a low TDS stream as a permeate from any of the one or more concentration operations, wherein the low TDS stream is recycled or used as fresh water.

The invention discloses an aluminum sulfate crystal production and preparation process and device, and relates to the technical field of aluminum sulfate crystal production and preparation. The device comprises a bottom plate and an evaporative crystallization mechanism, a collecting mechanism is slidably clamped on one side of the top end of the bottom plate, symmetrically-distributed fixing frames are fixedly installed on one side of the top end of the bottom plate, a buffering mechanism is fixedly installed at the top ends of the fixing frames, and a reaction kettle mechanism is fixedly installed on one side of the top end of the buffering mechanism. A filtering mechanism is fixedly mounted on the side, away from the reaction kettle mechanism, of the top end of the buffering mechanism, a neutralizing mechanism is fixedly mounted in the middle of the top end of the bottom plate, and an evaporative crystallization mechanism is fixedly mounted on one side of the top end of the bottom plate. By arranging the filtering mechanism, a first rotating motor is controlled to be started, the driving end of the first rotating motor rotates to drive a first bevel gear to rotate, the first bevel gear rotates to drive an engaged second bevel gear to rotate, and the second bevel gear rotates to drive a first rotating rod to rotate.

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

This invention belongs to the field of cryo-crystallization technology, specifically relating to a cryo-crystallization system and method, including a crystallizer and heat exchange pipelines. The crystallizer includes a tank, an air inlet, an air outlet, a feed inlet, and a discharge outlet disposed on the tank. The flow direction of the gas inside the tank is opposite to the flow direction of the liquid inside the tank. The heat exchange pipelines are equipped with a heat exchange device and a pressurization device, the heat exchange device being connected to a cold source. This invention, through optimization of the cryo-crystallization system and method, cleverly utilizes high-pressure gas as a heat transfer carrier. The flowing high-pressure, low-temperature gas conducts heat between the heat exchanger and the solution, with direct contact between the gas flow and the solution for heat transfer, avoiding direct contact between the solution and the heat exchanger wall. The problems of heat exchanger corrosion and surface icing (wall formation) can be fundamentally solved, improving the production efficiency of the cryo-crystallization process and reducing the manufacturing cost of the heat exchanger.

The invention discloses a built-in calcium fluoride crystallizer based on a coagulative precipitation tank, a first guide cylinder and a second guide cylinder are respectively fixed on opposite side walls in the coagulative precipitation tank, a fluorine-containing wastewater inlet pipeline conveys fluorine-containing wastewater into the first guide cylinder, a calcium-containing medicament inlet pipeline conveys a calcium-containing medicament into the second guide cylinder, and the first guide cylinder and the second guide cylinder are communicated with each other. The first propeller and the second propeller are fixed in the first guide cylinder and the second guide cylinder respectively, the first propeller vertically pushes flow downwards, the second propeller vertically pushes flow upwards, the stirrer can stir liquid in the coagulating basin, and the crystal discharging device can regularly discharge crystal precipitates at the bottom of the coagulating basin into the cyclone separator. The cyclone separator can perform cyclone separation on large-particle crystals and small-particle crystals, the large-particle crystals are discharged from a crystal outlet of the cyclone separator, and the small-particle crystals are discharged from a water outlet of the cyclone separator along with water flow and enter the coagulating basin. The medicament cost is reduced, and the improvement cost is low.

In a general aspect, a carbon dioxide (CO2) removal system uses geothermal energy. In some implementations, a method to remove CO2 gas from a gaseous feed includes directing a gaseous feed to interact with an alkaline capture solution in a first gas-liquid contactor. A first portion of CO2 from the gaseous feed dissolves into the alkaline capture solution to form a CO2-rich alkaline capture solution. Steam is generated using heat from a geothermal heat source, and the steam heats the CO2-rich alkaline capture solution in a second gas-liquid contactor. A second portion of the CO2 is separated from the CO2-rich alkaline capture solution in the second gas-liquid contactor to form a CO2-lean alkaline capture solution. The CO2-lean alkaline capture solution is directed to the first gas-liquid contactor.