WO2016197425A1 - 连续化水热法制备亚微米材料的装置系统及其制备工艺 - Google Patents

连续化水热法制备亚微米材料的装置系统及其制备工艺 Download PDF

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WO2016197425A1
WO2016197425A1 PCT/CN2015/083024 CN2015083024W WO2016197425A1 WO 2016197425 A1 WO2016197425 A1 WO 2016197425A1 CN 2015083024 W CN2015083024 W CN 2015083024W WO 2016197425 A1 WO2016197425 A1 WO 2016197425A1
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crystallizer
slurry
preparing
submicron
hydrothermal method
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PCT/CN2015/083024
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English (en)
French (fr)
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徐程浩
杨德建
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张家港合志纳米科技有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/02—Crystallisation from solutions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C01B25/16—Oxyacids of phosphorus; Salts thereof
    • C01B25/26—Phosphates
    • C01B25/45—Phosphates containing plural metal, or metal and ammonium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/04—Oxides; Hydroxides
    • C01G23/047—Titanium dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/04—Oxides; Hydroxides
    • C01G23/047—Titanium dioxide
    • C01G23/053—Producing by wet processes, e.g. hydrolysing titanium salts

Definitions

  • the invention relates to a liquid phase preparation process of a submicron material, in particular to a device system for continuously preparing a submicron material by hydrothermal method and a preparation process thereof.
  • Ultrafine powder technology is an emerging discipline developed in the mid-1970s, and ultrafine powder is used in almost all industries of the national economy. It is the basis for transforming and promoting the development of emerging industries such as paint coatings, information recording media, fine ceramics, electronic technology, new materials and biotechnology. It is the starting point of modern high-tech and has become the focus of research in various countries. With the ultra-fine refinement of materials, the surface electronic structure and crystal structure have changed, resulting in surface effects, small size effects, quantum effects and macroscopic quantum tunneling effects that block materials do not have, thus making ultrafine powders and conventional Granular materials have a series of excellent physical and chemical properties. These unique physical and chemical properties make it widely used in many fields such as electronics, chemistry, life sciences, and medicine.
  • nm is a cluster of atoms
  • 1 nm to 100 nm is a nanometer scale space
  • 100 nm to 1 ⁇ m is a submicron system
  • 1 ⁇ m to 10 ⁇ m is a fine powder
  • 10 ⁇ m to 45 ⁇ m is a fine powder.
  • Submicron materials are an important system in ultrafine materials, and can be divided into deep submicron (100nm ⁇ 500nm) and submicron (500nm ⁇ 1 ⁇ m).
  • an ultrafine powder 70% less than 1 ⁇ m, belonging to submicron powder, and 30% larger than 1 ⁇ m is a micron powder, how to determine whether the powder is a micron or submicron powder.
  • the volume fraction of D95 particle size or the volume fraction of D97 particle size, or even the volume fraction of D50 particle size is less than a certain value is defined as belonging to micron powder or submicron powder or nanometer. Powder.
  • the submicron-sized powder in this patent uses D50, PDI (particle size distribution coefficient), and three indexes of D97 ⁇ 1 ⁇ m to determine the particle size system of the product.
  • Ultrafine materials have excellent physicochemical properties, and these properties are affected by the size and morphology of ultrafine materials. Therefore, industrialization to achieve its control synthesis and study the relationship between its structure and properties are important for basic research and technical applications. significance.
  • Hydrothermal method is liquid phase An important method for the preparation of ultrafine materials by the reaction crystallization process.
  • the hydrothermal crystallization method uses an aqueous solution as the reaction system to create a relative by heating and pressurizing the reaction system (or autogenous vapor pressure).
  • the high-temperature, high-pressure reaction environment makes it an effective method for dissolving substances that are usually insoluble or insoluble, chemical reactions, and recrystallization to perform inorganic synthesis and material processing.
  • the product has stable performance, simple operation, controllable process and product quality, and the prepared product powder has uniform phase, high purity, small particle size and uniform distribution, and is suitable for preparation of ultra-fine functional materials.
  • Liquid-phase hydrothermal reaction The crystallization process consists of two processes, chemical and crystallization, involving chemical reactions, crystal nucleation, crystal growth, and secondary processes of crystals (aggregation, growth dispersion, maturation, etc.), and chemical reactions produce supersaturation.
  • the speed of the chemical reaction and the accompanying change in the pH of the solution directly affect the crystallization process.
  • the chemical reaction process also involves the dissolution rate of the precursor, and the dissolution rate is related to the particle size of the precursor, the heating rate, etc., the crystallization process and the supersaturation and its distribution.
  • the uniformity is closely related.
  • the invention provides a device system for continuously preparing hydrothermal method for preparing submicron materials and a preparation process thereof, and the device system and the preparation process solve the problem that the device and the process technology for preparing submicron materials by continuous hydrothermal method are immature and the crystallization efficiency is low. , easy to reunite and other issues, suitable for sub-micron materials industry continuous hydrothermal production.
  • a device system for continuously preparing hydrothermally prepared submicron materials comprising a first batching kettle, a second batching kettle, a preheater, a first crystallizer, a second crystallizer, and a heat exchanger Device.
  • the first batching tank is sequentially connected to the first feed pump and the preheater through a pipeline
  • the second batching tank is connected to the second feed pump through a pipeline
  • the preheater and the second feed pump are both connected to the first crystallizer through the pipeline Feed inlet.
  • the discharge port of the first crystallizer is connected to the inlet of the second crystallizer through a pipeline, and the discharge port of the second crystallizer is connected to the inlet of the heat exchanger through a pipeline, and the outlet of the heat exchanger is divided into two.
  • One outlet of the heat exchanger communicates with the outer circulation unit and then communicates with the inlet of the second crystallizer, and the other outlet of the heat exchanger communicates with the post-processing unit and then communicates with the slurry collector.
  • the first crystallizer is a tubular reaction crystallizer
  • the second crystallizer is a continuous reaction crystallizer.
  • the beneficial effect is that, due to the addition of the preheater, the solution accommodated in the first batching kettle can be heated in advance to achieve rapid temperature rise.
  • the addition of the first crystallizer allows pre-mixing and pre-nucleation of the reaction solution, which facilitates better crystallization and control of particle size distribution in the second crystallizer. Since the heat exchanger is connected outside the second crystallizer, the solution can be supersaturated after entering the heat exchanger, which can reduce the cost of the device to produce supersaturation.
  • the external circulation system is provided to increase crystallization efficiency and crystallinity.
  • the tubular reaction crystallizer and the continuous reaction crystallizer are combined in series, which can better realize homogeneous nucleation, growth and avoidance of submicron crystals under high supersaturation.
  • the crystallinity of the submicron particles is increased under the premise of aggregation growth.
  • the second crystallizer is a DTB type crystallizer.
  • the beneficial effect is that since the DTB crystallizer is a highly efficient professional crystallizer, it is widely used in industrial crystallization fields such as cooling and vacuum, and has a good internal flow field, small supersaturation and uniformity, and further crystallinity for further crystallization. Provide a mild condition.
  • the tubular reaction crystallizer is composed of a plurality of pipe mixers having the same inner diameter, and the tubular reaction crystallizer has a diameter of from DN25 to DN125 mm.
  • the beneficial effect is that since the tubular reaction crystallizer is composed of a multi-stage pipeline mixer, it can not only reduce The manufacturing cost of the tubular reaction crystallizer is also easy to remove and wash, and the total length and diameter of the tubular crystallizer can be flexibly adjusted according to the needs of the reaction solution.
  • the outer circulation unit comprises a circulation pump.
  • the aftertreatment unit includes a condenser, a filter, and a discharge valve that are in communication.
  • the beneficial effect is that the circulation pump can power the outer circulation.
  • the condenser can be quickly cooled, and the filter can filter out crystal clusters that grow up due to aggregation, ensuring uniformity of product particle size.
  • the outer circulation unit further includes a hydrodynamic ultrasonic generator disposed between the circulation pump and the second crystallizer.
  • the discharge valve is a back pressure valve. The beneficial effect is that since the hydrodynamic transducer relies on the high speed of the vibrating reed to generate a hydrodynamic cavitation effect, the particles can be dispersed to avoid aggregate growth.
  • the back pressure valve can flexibly control the discharge amount, and the back pressure valve is low in price, which is suitable for industrial production.
  • a flow meter is provided in the vicinity of the first feed pump, the second feed pump, and the circulation pump, and a pH detector and a pH feed liquid adjustment are provided on the outer circulation line of the second crystallizer. valve.
  • the beneficial effect is that the flow rate is conveniently monitored due to the increased flow meter. Since the pH of the solution changes during the crystallization process, the pH detector is convenient to monitor the pH of the solution, and the pH is increased.
  • the feed liquid regulating valve is used to adjust the pH of the solution in real time, and the solution particles can be controlled. Surface zeta potential to avoid particle agglomeration.
  • a process for preparing a submicron material by a hydrothermal process which uses the device system of the above embodiment, the process comprising the following steps:
  • the first raw material liquid contained in the first batching tank is sent to the preheater to be preheated to a certain temperature after being transported by the first feed pump, and the second raw material liquid contained in the second batching tank is transported by the second feed pump and
  • the preheated first raw material liquid enters the first crystallizer in a certain volume ratio to obtain a slurry, and the slurry flows in the first crystallizer at a certain flow rate for a period of time, and then enters the second crystallizer;
  • the slurry enters the second crystallizer for crystallization, and part of the slurry flows out from the discharge port of the second crystallizer, exchanges heat through the heat exchanger, is driven by the circulation pump and is mixed with the slurry from the first crystallizer. Re-entering the second crystallizer to form an outer loop, and after reacting for a period of time in the second crystallizer, obtaining a suspended crystal slurry;
  • the suspended crystal slurry flows out from the discharge port of the second crystallizer, exchanges heat through the heat exchanger, and the condenser condenses to a certain temperature, and then filters a small amount of crystal clusters grown by aggregation through the filter.
  • the homogenization of the product particle size is ensured; under the action of the discharge valve, the crystal slurry is stably discharged and collected in the slurry collector.
  • the first raw material liquid is a precursor solution
  • the second raw material liquid is an aqueous solution or another precursor solution
  • the pH of the crystal slurry in the second crystallizer is controlled to control the zeta potential of the suspended crystal surface, Avoid particle aggregation growth of the crystal slurry.
  • the utility model has the beneficial effects that when the second raw material liquid and the preheated first raw material liquid are mixed in the first crystallizer, since the temperature of the first raw material liquid is high, the first raw material liquid can be heated and heated rapidly at the instant of mixing. , increase the degree of supersaturation.
  • the raw material liquid is initially crystallized in the first crystallizer to generate a large amount of submicron-sized particles, it is further crystallized into the second crystallizer, and part of the slurry enters the heat exchanger to generate supersaturation, which facilitates nucleation and grain growth. .
  • the slurry is externally circulated outside the second crystallizer by a circulation pump to improve crystallization efficiency and crystallinity.
  • the crystal slurry is cooled by a condenser to quickly cool down and avoid particle agglomeration.
  • the preheating temperature of the first feedstock liquid through the preheater is from 100 to 350 °C.
  • the second raw material liquid and the preheated first raw material liquid enter the first crystallizer in a volume ratio of 1:1 to 1:10.
  • the beneficial effect is that by controlling the ratio of the raw material liquid, the suspension density or the number density of the particles can be controlled to avoid particle agglomeration.
  • the slurry has a flow rate in the first crystallization tube of 0.25 to 1.0 m/s and a residence time of 1 to 30 minutes.
  • the reaction time in the second crystallizer is 0.5 to 24 hours, and the temperature after passing through the condenser is 25 to 60 °C.
  • the filter has a filter accuracy of 1.0 ⁇ m. The beneficial effect is that the suspension density or the number density of the first crystallizer is controlled by controlling the flow rate and the reaction time to avoid particle agglomeration.
  • the flow rate inside the control tube can also avoid the crusting of the inner wall of the tube.
  • the purpose of the filter is to control the particle size of submicron products.
  • the reaction crystallization control principle of the present invention is: according to the mechanism of the hydrothermal reaction crystallization process, separating nucleation and growth, increasing the nucleation rate, crystallization (aging) under low supersaturation and controlling ultrafine particles by chemical and physical methods. Aggregation, continuous production of sub-micron materials with uniform particle size distribution.
  • FIG. 1 is a schematic view showing a process flow of a device system and a preparation process for preparing a submicron material by a hydrothermal method according to an embodiment of the present invention
  • Example 2 is a particle size distribution diagram of submicron titanium dioxide prepared in Example 1;
  • Example 3 is a particle size distribution diagram of submicron lithium iron phosphate prepared in Example 3.
  • a system for continuously preparing hydrothermally prepared submicron materials comprising a first batching tank 1, a second batching tank 2, a preheater 5, a first crystallizer 6, a second crystallizer 7, and a heat exchanger 9 .
  • the first batching tank 1 and the second batching tank 2 are respectively used for containing the first solution and the second solution.
  • the first batching tank 1 is sequentially connected to the first feed pump 3 and the preheater 5 through a pipeline, and the second batching tank 2 is connected to the second feed pump 4 through a pipeline, and the preheater 5 and the second feed pump 4 are both passed through the pipeline.
  • the inlet of the first crystallizer 6 is connected.
  • the discharge port of the first crystallizer 6 is connected to the inlet of the second crystallizer 7 through a line
  • the discharge port of the second crystallizer 7 is connected to the inlet of the heat exchanger 9 through a line
  • the outlet of the heat exchanger 9 has two outlets.
  • An outlet of the heat exchanger 9 re-enters the inlet of the second crystallizer 7 through the outer circulation unit; the other outlet of the heat exchanger 9 is connected to the post-treatment unit via the pipeline to reconnect the slurry collector 15.
  • the second crystallizer 7 is a continuous type reaction crystallizer, preferably a DTB type crystallizer. An agitator or a propeller may be added to the second crystallizer 7 to push the paddle in the mold to move upward.
  • the first crystallizer 6 may be a tubular reaction crystallizer, and the tubular reaction crystallizer may be composed of a plurality of pipe mixers having the same inner diameter, and the pipe mixer may be assembled into any structure, usually, a tubular reaction crystallizer.
  • the structure is a U-shaped structure.
  • the tubular reaction crystallizer is arranged in a vertical or horizontal manner. Preferably, the tubular reaction crystallizer is in a horizontal arrangement.
  • the tube diameter of the tubular reaction crystallizer is preferably DN25 to DN125 mm.
  • the outer circulation unit includes a circulation pump 10.
  • the aftertreatment unit includes a condenser 12, a filter 13 and a discharge valve 14 that are in communication.
  • the circulation pump 10 can provide power to the outer circulation unit.
  • the condenser 12 can be rapidly cooled, and the filter 13 can filter out crystal clusters which grow up due to aggregation, thereby ensuring uniformity of product particle size, and the discharge valve 14 ensures stable discharge.
  • the outer circulation unit further comprises a hydrodynamic ultrasonic generator 11 between the circulation pump 10 and the second crystallizer 7.
  • the hydrodynamic transducer 11 generates a hydrodynamic cavitation effect by virtue of the high speed vibration of the vibrating reed, which can disperse the particles and avoid agglomeration.
  • the slurry passing through the hydrodynamic generator 11 enters the second crystallizer 7 together with the slurry from the first crystallizer 6, for continuous circulation flow.
  • the discharge valve 14 can be a discharge pump or a back pressure valve.
  • the discharge valve 14 is a back pressure valve.
  • a flow meter is arranged in the vicinity of the first feed pump 3, the second feed pump 4 and the circulation pump 10, and a pH detector is arranged on the outer circulation line of the second crystallizer 7 to detect the external circulation system.
  • the external circulation pipeline is also connected with a pH feed liquid regulating valve 8 for controlling the entry amount of the engineering liquid PL, and the engineering liquid PL is an engineering acid liquid or an alkali liquid.
  • the pH feed liquid regulating valve 8 is preferably installed on a branch line between the second crystallizer 7 and the heat exchanger 9.
  • a preparation process for preparing a submicron material by a hydrothermal method comprising the following steps:
  • the first raw material liquid contained in the first batching tank 1 is transported by the first feed pump 3, then enters the preheater 5 to be preheated to a certain temperature, and the second raw material liquid contained in the second batching tank 2 is passed through the second feed pump. 4 transporting and entering the first crystallizer 6 with a pre-heated first raw material liquid in a certain volume ratio to obtain a slurry, and the slurry flows in the first crystallizer 6 at a certain flow rate for a period of time, and then enters the second crystal. 6
  • the slurry enters the second crystallizer 6 for crystallization, and part of the slurry flows out from the discharge port of the second crystallizer 6, and is exchanged by the heat exchanger 9, driven by the circulation pump 10 and with the first crystallizer 6 After mixing, the slurry enters the second crystallizer 7 again to form an outer cycle, and after reacting for a period of time in the second crystallizer 7, a suspension crystal slurry is obtained;
  • the suspended crystal slurry flows out from the discharge port of the second crystallizer 7, and is exchanged by the heat exchanger 9, and after the condenser 12 is condensed to a certain temperature, a small amount of crystal clusters grown by aggregation are filtered through the filter 13 to ensure The homogeneity of the product particle size is achieved; under the action of the discharge valve 14, the crystal slurry is stably discharged and collected in the slurry collector 15.
  • the first raw material liquid is a precursor solution
  • the second raw material liquid is an aqueous solution or another precursor solution, preferably an aqueous solution.
  • the pH of the crystal slurry in the second crystallizer 7 is adjusted, and the amount of the engineering liquid PL can be controlled by adjusting the pH feed liquid regulating valve 8 to control the zeta potential of the suspended crystal surface to avoid the crystal slurry.
  • the particles aggregate and grow.
  • the preheating temperature of the first raw material liquid through the preheater 5 is 100 to 350 ° C.
  • the second raw material liquid and the preheated first raw material liquid are in a volume ratio of 1:1 to 1:10.
  • the example enters the first crystallizer.
  • the flow rate of the slurry in the first crystallization tube 6 is 0.25-1.0 m/s, and the residence time is 1-30 min.
  • reaction temperature of the second crystallizer 7 is not greater than the reaction temperature of the first crystallizer 8.
  • the reaction time in the second crystallizer 8 is 0.5 to 24 hours
  • the temperature after passing through the condenser 12 is 25 to 60 ° C
  • the filter precision of the filter is 1.0 ⁇ m.
  • the first raw material liquid is a titanium sulfate liquid precursor solution
  • the second raw material liquid is an aqueous solution.
  • concentration of TiO 2 in the precursor solution of titanium sulphate solution is 260g/L
  • the value of acidity F is 2.0
  • the ratio of iron to titanium is 0.21
  • the outlet temperature of the preheated water through the preheater 5 is 125 ° C, and the volume ratio of the titanium sulfate liquid precursor solution and the preheated water entering the first crystallizer 6 is 1:4, and the diameter of the first crystallizer 6 For DN25.
  • the flow rate of the precursor solution was 250 L/h, and the flow rate of water was 1000 L/h.
  • the flow rate of the first crystallizer 6 is 0.75 m/s, the residence time is 5 min, the pipeline arrangement is arranged in a horizontal U-shape, the total length of the pipeline is 200 m, the temperature inside the tube is maintained at 108 ° C, and the temperature of the second crystallizer 7 is 105 ° C.
  • the residence time in the second crystallizer 7 was 5 h.
  • the isoelectric point of TiO 2 is about 4.3, and the pH of the suspended crystal slurry in the second crystallizer 7 is controlled to 7.2, away from the isoelectric point, to avoid particle aggregation growth, and the control pressure of the discharge valve 14 is 0.1 MPa, the condenser 12
  • the outlet temperature was 40 ° C, and the filter screen of the filter 14 was 1.0 ⁇ m.
  • the metatitanic acid precipitate collected by the above preparation is subjected to post-calcination to obtain submicron titanium dioxide.
  • 2 is a particle size distribution diagram of the prepared submicron titanium dioxide.
  • the preparation process of the sub-micron titanium dioxide by the continuous hydrothermal method is as follows:
  • the first raw material liquid is a titanium sulfate liquid precursor solution
  • the second raw material liquid is an aqueous solution.
  • concentration of TiO 2 in the precursor solution of titanium sulphate solution is 300g/L
  • the value of acidity F is 1.8
  • the ratio of iron to titanium is 0.21
  • the outlet temperature of the preheated water through the preheater 5 is 180 ° C, and the volume ratio of the titanium sulfate liquid precursor solution and the preheated water entering the first crystallizer 6 is 1:1, and the diameter of the first crystallizer 6 is For DN125.
  • the flow rate of the precursor solution was 5,500 L/h, and the flow rate of water was 5,500 L/h.
  • the flow rate of the first crystallizer 6 is 0.25 m/s, the residence time is 30 min, and the pipe arrangement of the tubular reaction crystallizer is arranged in a horizontal U-shape, the total length of the pipe is 480 m, and the temperature inside the pipe is maintained at 105 ° C, the second crystallizer 7 The temperature was 102 ° C, and the residence time in the second crystallizer 7 was 24 h.
  • the isoelectric point of TiO 2 is about 4.3, and the pH of the suspended crystal slurry in the second crystallizer 7 is controlled to be 7.5, away from the isoelectric point, to avoid particle aggregation growth, and the control pressure of the discharge valve 14 is 0.1 MPa, the condenser 12
  • the outlet temperature was 25 ° C, and the filter screen of the filter 14 was 1.0 ⁇ m.
  • the preparation process of submicron lithium iron phosphate by hydrothermal method is as follows:
  • the first raw material liquid is a precursor solution
  • the second raw material liquid is an aqueous solution.
  • the precursor solution was a suspension of 85% phosphoric acid, 1.5 mol/L LiOH aqueous solution and 0.5 mol/L FeSO 4 aqueous solution which was smoothly arranged according to a certain addition.
  • the XRD analysis showed that the precipitate phase was Li 3 PO 4 and Fe 3 ( PO4) 2 ⁇ 8H 2 O, the pH of the suspension was 6.0 and the temperature was 35 °C.
  • the outlet temperature of the preheated water through the preheater 5 is 220 ° C
  • the volume ratio of the precursor solution to the preheated water is 1:5
  • the diameter of the pipe is DN25
  • the flow rate of the precursor is 200 L/h
  • the flow rate of water is 1000 L/ h.
  • the flow rate of the first crystallizer 6 is 0.65 m/s and the residence time is 10 min.
  • the pipe arrangement of the first crystallizer 6 is arranged in a horizontal U-shape, the total length of the pipe is 400 m, and the temperature inside the pipe is maintained at 185 ° C, and the second crystallizer 7
  • the temperature is 180 ° C
  • the residence time of the second crystallizer 7 is 3 h
  • the isoelectric point of LiFePO 4 is about 3.55
  • the pH of the suspended crystal slurry in the second crystallizer 7 is controlled to 6.8, away from the isoelectric point, avoiding particles.
  • Aggregate growth the control pressure of the discharge valve 14 was 1.0 MPa, the outlet temperature of the condenser 12 was 60 ° C, and the sieve of the filter 13 was 1.0 ⁇ m.
  • the first raw material liquid is a precursor solution
  • the second raw material liquid is an aqueous solution.
  • the precursor solution was a suspension of 85% phosphoric acid, 2.5 mol/L LiOH aqueous solution and 1.0 mol/L FeSO 4 aqueous solution which were smoothly arranged according to a certain addition.
  • the XRD analysis showed that the precipitate phase was Li 3 PO 4 and Fe 3 ( PO4) 2 ⁇ 8H 2 O, the pH of the suspension was 6.2 and the temperature was 60 °C.
  • the outlet temperature of the preheated water through the preheater 5 is 200 ° C
  • the volume ratio of the precursor solution to the preheated water is 1:10
  • the diameter of the pipe is DN25
  • the flow rate of the precursor is 160 L/h
  • the flow rate of water is 1600 L/ h.
  • the first crystallizer 6 has a flow rate of 1.0 m/s in the tube and a residence time of 5 min.
  • the pipe arrangement of the first crystallizer 6 is arranged in a horizontal U-shape, the total length of the pipe is 300 m, and the temperature inside the pipe is maintained at 187 ° C, and the second crystallizer 7
  • the temperature is 175 ° C
  • the residence time of the second crystallizer 7 is 2.5 h
  • the isoelectric point of LiFePO 4 is about 3.55
  • the pH of the suspended crystal slurry in the second crystallizer 7 is controlled to 6.8, away from the isoelectric point, avoiding
  • the particles were aggregated and grown
  • the control pressure of the discharge valve 14 was 0.9 MPa
  • the outlet temperature of the condenser 12 was 50 ° C
  • the sieve of the filter 13 was 1.0 ⁇ m.

Abstract

一种连续化水热法制备亚微米材料的装置系统及其制备工艺。该装置系统包括第一配料釜（1）、第二配料釜（2）、预热器（5）、第一结晶器（6）和第二结晶器（7）。其中，第一配料釜（1）通过第一进料泵（3）和预热器（5）连通第一结晶器（6），第二配料釜（2）通过第二进料泵（4）连通第一结晶器（6）。第一结晶器（6）连通第二结晶器（7），第二结晶器（7）的出料口连通换热器（9）的入口，换热器（9）的出口分为两个，一个连通外循环单元再连通第二结晶器（7）的入口，而另一个则连通后处理单元与料浆收集器（15）。其中，第一结晶器（6）为管式反应结晶器，第二结晶器（7）为连续型结晶器。该制备工艺采用该装置系统，不仅装置成本低，同时可连续制备粒度分布均匀且结晶度高的亚微米材料，适用于工业化生产。

Description

连续化水热法制备亚微米材料的装置系统及其制备工艺 技术领域
本发明涉及亚微米材料的液相法制备工艺，特别涉及一种连续化水热法制备亚微米材料的装置系统及其制备工艺。
背景技术
超细粉体技术是20世纪70年代中期发展起来的新兴学科，超细粉体几乎应用于国民经济的所有行业。它是改造和促进油漆涂料、信息纪录介质、精细陶瓷、电子技术、新材料和生物技术等新兴产业发展的基础，是现代高新技术的起点，日趋成为各国研究的重点。随着物质的超细化，其表面电子结构和晶体结构发生了变化，产生了块状材料不具备的表面效应，小尺寸效应，量子效应和宏观量子隧道效应，从而使超细粉体与常规颗粒材料相比具有一系列优异的物理、化学性质。而这些独特的物理化学性质使得其在电子学、化学化工、生命科学、医学等众多领域有着广泛的应用前景。依据材料粒径的不同，国际上公认小于1nm为原子团簇，1nm～100nm为纳米尺度空间，100nm～1μm为亚微米体系，1μm～10μm为微粉体，10μm～45μm为细粉体。亚微米级材料是超细材料中的一个重要体系，又可分为深亚微米级(100nm～500nm)和亚微米级(500nm～1μm)。
对于某一特定的超细粉体，仅上述划分是不够准确的，一般超细粉体的粒径分布呈正态分布规律。例如：一种超细粉体，有70％小于1μm，属于亚微米粉体，还有30％大于1μm属于微米粉体，如何确定上述粉体是微米或者亚微米粉体。应该从某种物料的应用角度出发，采用D95粒径的体积分数或D97粒径的体积分数，甚至D50粒径的体积分数小于某一值来定义是属于微米粉体或亚微米粉体或纳米粉体。本专利中的亚微米级粉体采用D50、PDI(粒径分布系数)，和D97＜1μm的三个指标共同来确定产品的粒径体系。
超细材料具有优异的物化性质，而这些性质又受到超细材料的尺寸、形貌结构的影响，因此工业化实现其控制合成及研究其结构与性质之间关系对于基础研究和技术应用都具有重要意义。水热法是液相 反应结晶工艺制备超细材料的一种重要方法，水热结晶法是在特制的密闭反应器中，采用水溶液作为反应体系，通过对反应体系加热、加压(或自生蒸气压)，创造一个相对高温、高压的反应环境，使得通常难溶或不溶的物质溶解，发生化学反应，并且重结晶而进行无机合成与材料处理的一种有效方法。产品性能稳定，操作简单，过程和产品质量可控，制备的产品粉末物相均一，纯度高、颗粒粒径小而分布均匀，适用于超细功能材料的制备。
连续水热法作为低成本制备工艺已受到全世界越来越多的关注，国内还没有连续化生产的相关报道，国内采用的多数方法为釜式压力容器的间歇操作，而这样的操作存在着：①壁面传热系数低，加热时间长，能耗高；②料浆中粉体颗粒易于粘壁，更加降低传热效率；③高温高压条件下，釜体密封困难，釜体局部压力、温度可能出现不均匀现象，安全性较低；④大规模生产设备与小试、中试装置产品性能差异大。
连续水热法之所以在实际应用中还没有被广发采纳，我们认为主要在于对液相水热反应结晶过程的机理以及实际工程化过程中的如何控制相关参数来控制晶体产品的物化性能。液相水热反应结晶过程是一个化学和结晶两个过程组成，涉及化学反应、晶体成核、晶体生长以及晶体的二次过程(聚集、生长分散、熟化等等)，化学反应产生过饱和度，化学反应的快慢且伴随着的溶液pH值的变化等等都直接影响着结晶过程；其次，由于产品的粒径较小，存在着较大的比表面，晶体非常容易发生聚集生长；再其次，由于前驱体的特殊性，影响化学反应过程的还涉及到前驱体的溶解速率问题，而溶解速率的快慢又与前驱体的粒度，升温速率等等相关，结晶过程与过饱和度及其分布的均匀性密切相关。总而言之，这是一个相当复杂的多相过程，要求我们在实际的装备设计上充分的屏蔽掉一些对产品物化性能影响波动较大的因素(将一些参数值稳定在最佳范围，避免其对结晶过程产生重大影响)，将重点放在对结晶的控制上，尽量做到控制单一或几个因素就能稳定结晶产品。简言之，高过饱和度且分布均匀同时控制超细颗粒表面电位是制备均匀亚微米材料的关键。
发明内容
本发明提供了一种连续化水热法制备亚微米材料的装置系统及其制备工艺，该装置系统及制备工艺解决了连续水热法制备亚微米材料的装置及工艺技术不成熟、结晶效率低、易团聚等问题，适用于亚微米材料工业连续化水热法生产。
根据本发明的一个方面，提供一种连续化水热法制备亚微米材料的装置系统，包括第一配料釜、第二配料釜、预热器、第一结晶器、第二结晶器和换热器。其中，第一配料釜通过管线依次连通第一进料泵和预热器，第二配料釜通过管线连通第二进料泵，预热器和第二进料泵均通过管线连通第一结晶器的入料口。第一结晶器的出料口通过管线连通第二结晶器的入料口，第二结晶器的出料口通过管线连通所述换热器的入口，换热器的出口分为两个，换热器的一个出口连通外循环单元再连通第二结晶器的入口，换热器的另一个出口连通后处理单元再连通料浆收集器。其中，第一结晶器为管式反应结晶器，第二结晶器为连续型反应结晶器。
其有益效果是，由于增加了预热器，可提前对容置于第一配料釜中的溶液进行加热，实现快速升温。增加的第一结晶器可实现反应溶液的预混合和预成核，有利于在第二结晶器中更好的结晶及控制粒径分布。由于第二结晶器外连通有换热器，溶液进入换热器后可产生过饱和度，可降低装置对产生过饱和度的成本。设置的外循环系统可提高结晶效率及结晶度。此外，依据纳米晶体的反应结晶机理，将管式反应结晶器与连续型反应结晶器串联结合起来，可较好的实现地亚微米晶体在高过饱和度下均相成核、生长以及在避免聚集生长的前提下提高亚微米颗粒的结晶度。
在一些实施方式中，第二结晶器为DTB型结晶器。其有益效果是，由于DTB结晶器是一种高效专业结晶器，广泛应用于冷却、真空等工业结晶领域，其内部具有良好的流场，过饱和度小且均匀，为进一步晶化提高结晶度提供一个温和的条件。
在一些实施方式中，管式反应结晶器为由多段具有相同内径的管道混合器组成，管式反应结晶器的管径为DN25～DN125mm。其有益效果是，由于管式反应结晶器是由多段管道混合器组成，不仅可降低 管式反应结晶器的制造成本，也方便拆洗，同时也可根据反应溶液的需要，灵活的调整管式结晶器的总长度及管径尺寸。
在一些实施方式中，外循环单元包括循环泵。后处理单元包括依次连通的冷凝器、过滤器和出料阀。其有益效果是，循环泵可为外循环提供动力。冷凝器可快速降温，过滤器可过滤掉因聚集而长大的晶体团簇，保证了产品粒度的均一化。
在一些实施方式中，外循环单元还包括水力超声发生器，水力超声发生器设于循环泵与第二结晶器之间。出料阀为背压阀。其有益效果是，由于水力超声器依靠振动簧片的高速而振动产生水力空化效应，可将颗粒分散开，避免聚集生长。背压阀可灵活的控制出料量，且背压阀价格低，适用于工业生产使用。
在一些实施方式中，第一进料泵、第二进料泵和循环泵的附近均设有流量计，第二结晶器的外循环的管线上设有pH检测仪以及pH值进料液调节阀。其有益效果是，由于增加的流量计方便监测流量。由于在晶化过程中，溶液的pH随着反应的进行会发生改变，增加pH检测仪方便监测溶液的pH，增加pH值进料液调节阀用于实时的调节溶液的pH，可控制溶液颗粒表面Zeta电位，避免颗粒团聚。
根据本发明的另一个方面，提供了一种连续化水热法制备亚微米材料的制备工艺，该工艺使用上述实施方式中的装置系统，该工艺包括如下步骤：
盛装于第一配料釜的第一原料液经第一进料泵输送后进入预热器预热至一定温度，盛装于第二配料釜的第二原料液经第二进料泵输送并与经预热后的第一原料液按一定体积比例进入第一结晶器，得到料浆，料浆在第一结晶器中以一定的流速流动一段时间后，进入第二结晶器；
料浆进入第二结晶器进行晶化，部分料浆从第二结晶器的出料口流出，经换热器换热，在循环泵的驱动下并与来自第一结晶器的料浆混合后再次进入第二结晶器，构成一个外循环，在第二结晶器中反应一段时间后，得到悬浮晶浆；
悬浮晶浆从第二结晶器的出料口流出，经过换热器换热，冷凝器冷凝至一定温度后，通过过滤器滤除少量因聚集而长大的晶体团簇， 保证了产品粒度的均一化；在出料阀的作用下，晶浆稳定出料并收集于料浆收集器。
其中，第一原料液为前驱体溶液，第二原料液为水溶液或另一前驱体溶液；在晶化过程中，调控第二结晶器中的晶浆的pH以控制悬浮晶体表面的Zeta电位，避免晶浆的颗粒聚集生长。
其有益效果是，当第二原料液与经预热的第一原料液在第一结晶器中混合时，由于第一原料液的温度高，在混合瞬间可快速对第一原料液进行加热升温，提高过饱和度。原料液在第一结晶器中初步晶化产生大量亚微米级粒子后，进入第二结晶器中进一步晶化，部分料浆进入换热器产生过饱和度，便于晶核形成和晶粒长大。料浆通过循环泵在第二结晶器外进行外循环，可提高结晶效率及结晶度。晶浆经冷凝器冷却，可快速降温，避免颗粒团聚。
在一些实施方式中，第一原料液经预热器的预热温度为100～350℃。
在一些实施方式中，第二原料液与预热后的第一原料液按1∶1～1∶10的体积比例进入第一结晶器。其有益效果是，通过控制原料液的比例，可控制料浆中的悬浮密度或粒数密度，避免粒子团聚。
在一些实施方式中，料浆在第一结晶管管内的流速为0.25～1.0m/s，停留时间为1～30min。在第二结晶器的反应时间为0.5～24h，经冷凝器后的温度为25～60℃。过滤器的滤网精度为1.0μm。其有益效果是，通过控制流速和反应时间来控制第一结晶器内的悬浮密度或粒数密度，避免粒子团聚。此外，控制管内流速还可避免管内壁结疤现象。过滤器的作用是为了控制亚微米级产品的粒度。
本发明的反应结晶控制原理是：依据水热反应结晶过程的机理，将成核及生长分开，提高成核速率，在低过饱和度下晶化(熟化)并通过化学及物理方法控制超细粒子的聚集，连续制得粒度分布均匀的亚微米材料。
附图说明
图1为本发明一实施方式的一种连续化水热法制备亚微米材料的装置系统和制备工艺的工艺流程示意图；
图2为实施例1所制备的亚微米级钛白粉粒度分布图；
图3为实施例3所制备的的亚微米级磷酸铁锂粒度分布图。
具体实施方式
下面结合附图及具体实施例对本发明作进一步详细的说明。
参见图1为本发明一种连续化水热法制备亚微米材料的装置系统和制备工艺的工艺流程示意图。一种连续化水热法制备亚微米材料的装置系统，包括第一配料釜1、第二配料釜2、预热器5、第一结晶器6、第二结晶器7、和换热器9。其中，第一配料釜1和第二配料2釜分别用于盛装第一溶液和第二溶液。第一配料釜1通过管线依次连通第一进料泵3和预热器5，第二配料釜2通过管线连通第二进料泵4，预热器5和第二进料泵4均通过管线连通第一结晶器6的入料口。第一结晶器6的出料口通过管线连通第二结晶器7的入料口，第二结晶器7的出料口通过管线连通换热器9的入口，换热器9的出口有两个，换热器9的一个出口通过外循环单元再进入第二结晶器7的入口；换热器9的另一个出口通过管线连通后处理单元再连通料浆收集器15。
第二结晶器7为连续型反应结晶器，优选的为DTB型结晶器。第二结晶器7内可增设搅拌器或螺旋桨，以推动结晶器内料桨向上运动。第一结晶器6可为管式反应结晶器，管式反应结晶器可由多段具有相同内径的管道混合器组成不同长度，管道混合器可组装成任意结构，通常，管式反应结晶器所组成的结构为U型结构。管式反应结晶器为立式或卧式排布，优选的，管式反应结晶器为卧式排布。管式反应结晶器的管径优选的为DN25～DN125mm。
本实施方式中，外循环单元包括循环泵10。后处理单元包括依次连通的冷凝器12、过滤器13和出料阀14。由于循环泵10可为外循环单元提供动力。冷凝器12可快速降温，过滤器13可过滤掉因聚集而长大的晶体团簇，保证了产品粒度的均一化，出料阀14保证稳定出料。
为了避免外循环系统中的颗粒团聚，外循环单元还包括水力超声发生器11，水力超声发生器11在循环泵10与第二结晶器7的之间。 水力超声器11依靠振动簧片的高速而振动产生水力空化效应，可将颗粒分散开，避免团聚。经水力超声发生器11的料浆与来自第一结晶器6的料浆一起进入第二结晶器7中，进行连续循环流动。出料阀14可为出料泵或背压阀，优选的，出料阀14为背压阀。
为了方便控制，第一进料泵3、第二进料泵4和循环泵10的附近均设有流量计，第二结晶器7的外循环的管线上设有pH检测仪以检测外循环系统中的料浆的pH值。外循环的管线上还连接有pH值进料液调节阀8，用以控制工程液体PL的进入量，工程液体PL为工程用酸液或碱液。pH值进料液调节阀8优选的安装在第二结晶器7和换热器9之间的分支管线上。
一种连续化水热法制备亚微米材料的制备工艺，该工艺包括如下步骤：
盛装于第一配料釜1的第一原料液经第一进料泵3输送后进入预热器5预热至一定温度，盛装于第二配料釜2的第二原料液经第二进料泵4输送并与经预热后的第一原料液按一定体积比例进入第一结晶器6，得到料浆，料浆在第一结晶器6中以一定的流速流动一段时间后，进入第二结晶器6；
料浆进入第二结晶器6进行晶化，部分料浆从第二结晶器6的出料口流出，经换热器9换热，在循环泵10的驱动下并与来自第一结晶器6的料浆混合后再次进入第二结晶器7，构成一个外循环，在第二结晶器7中反应一段时间后，得到悬浮晶浆；
悬浮晶浆从第二结晶器7的出料口流出，经过换热器9换热，冷凝器12冷凝至一定温度后，通过过滤器13滤除少量因聚集而长大的晶体团簇，保证了产品粒度的均一化；在出料阀14的作用下，晶浆稳定出料并收集于料浆收集器15。
其中，第一原料液为前驱体溶液，第二原料液为水溶液或另一前驱体溶液，优选的为水溶液。在晶化过程中，调控第二结晶器7中的晶浆的pH，可通过调节pH值进料液调节阀8控制工程液体PL的进入量，以控制悬浮晶体表面的Zeta电位，避免晶浆的颗粒聚集生长。
可选的，第一原料液经预热器5的预热温度为100～350℃。
可选的，第二原料液与预热后的第一原料液按1∶1～1∶10的体积比 例进入第一结晶器。
可选的，料浆在第一结晶管6管内的流速为0.25～1.0m/s，停留时间为1～30min。
可选的，第二结晶器7的反应温度不大于所述第一结晶器8的反应温度。
可选的，在第二结晶器8的反应时间为0.5～24h，经冷凝器12后的温度为25～60℃，过滤器的滤网精度为1.0μm。
为了进一步说明本发明，下面结合实施例对本发明提供的连续化水热法制备亚微米材料的制备工艺做进一步详细地描述，但不能将它们理解为对本发明保护范围的限定。
实施例1
以硫酸法制备亚微米级钛白粉为例，连续化水热法制备亚微米钛白粉的制备工艺，如下：
第一原料液为硫酸钛液前驱体溶液，第二原料液为水溶液。硫酸钛液前驱体溶液中TiO2浓度260g/L，酸度系数F值(有效酸与总TiO2浓度的比值)为2.0，铁钛比(钛液中铁离子的浓度与总钛浓度的比值)为0.21，钛液稳定度＞500，澄清度较好，温度为40℃。经预热器5的预热水的出口温度为125℃，进入第一结晶器6中的硫酸钛液前驱体溶液与预热水的体积比例为1∶4，第一结晶器6的管径为DN25。前驱体溶液的流量为250L/h，水的流量为1000L/h。第一结晶器6的管内流速为0.75m/s，停留时间为5min，管道布置采用卧式U型排列，管道总长为200m，维持管内温度为108℃，第二结晶器7温度为105℃，在第二结晶器7的停留时间为5h。TiO2的等电点约为4.3，第二结晶器7内悬浮晶浆的pH值控制为7.2，远离等电点，避免颗粒聚集生长，出料阀14的控制压力为0.1MPa，冷凝器12出口温度为40℃，过滤器14的滤网为1.0μm。
将以上制备收集得到的偏钛酸沉淀经过后期煅烧后得到亚微米级钛白粉。参见图2为所制备的亚微米级钛白粉粒度分布图，产品的粒径D50＝271.3nm，PDI＝0.367，D97＝378.1nm。
实施例2
连续化水热法制备亚微米钛白粉的制备工艺，如下：
第一原料液为硫酸钛液前驱体溶液，第二原料液为水溶液。硫酸钛液前驱体溶液中TiO2浓度300g/L，酸度系数F值(有效酸与总TiO2浓度的比值)为1.8，铁钛比(钛液中铁离子的浓度与总钛浓度的比值)为0.21，钛液稳定度＞500，澄清度较好，温度为30℃。经预热器5的预热水的出口温度为180℃，进入第一结晶器6中的硫酸钛液前驱体溶液与预热水的体积比例为1∶1，第一结晶器6的管径为DN125。前驱体溶液的流量为5500L/h，水的流量为5500L/h。第一结晶器6的管内流速为0.25m/s，停留时间为30min，管式反应结晶器的管道布置采用卧式U型排列，管道总长为480m，维持管内温度为105℃，第二结晶器7温度为102℃，在第二结晶器7的停留时间为24h。TiO2的等电点约为4.3，第二结晶器7内悬浮晶浆的pH值控制为7.5，远离等电点，避免颗粒聚集生长，出料阀14的控制压力为0.1MPa，冷凝器12出口温度为25℃，过滤器14的滤网为1.0μm。
将以上制备收集得到的偏钛酸沉淀经过后期煅烧后得到亚微米级钛白粉，所制备的产品的粒径D50＝286.5nm，PDI＝0.335，D97＝352.6nm。
实施例3
以制备锂离子电池关键正极材料磷酸铁锂为例，连续化水热法制备亚微米磷酸铁锂的制备工艺，如下：
第一原料液为前驱体溶液，第二原料液为水溶液。前驱体溶液为85％磷酸、1.5mol/L LiOH水溶液和0.5mol/L FeSO4水溶液按照一定加料顺利配置而成的悬浊液，经过XRD分析可知沉淀物相为Li3PO4和Fe3(PO4)2·8H2O，悬浊液的pH值为6.0，温度为35℃。经预热器5的预热水的出口温度为220℃，前驱体溶液与预热水的体积比例为1∶5，管径为DN25，前驱体流量为200L/h，水的流量为1000L/h。第一结晶器6的管内流速为0.65m/s，停留时间为10min，第一结晶器6的管道布置采用卧式U型排列，管道总长为400m，维持管内温度为185℃，第二结晶器7温度为180℃，第二结晶器7的停留时间为3h，LiFePO4的等电点约为3.55，第二结晶器7内悬浮晶浆的pH值控制 为6.8，远离等电点，避免颗粒聚集生长，出料阀14的控制压力为1.0MPa，冷凝器12出口温度为60℃，过滤器13的滤网为1.0μm。参见图3为所制备的的亚微米级磷酸铁锂粒度分布图，产品粒径D50＝253.7nm，PDI＝0.168，D97＝342nm。
实施例4
连续化水热法制备亚微米磷酸铁锂的制备工艺，如下：
第一原料液为前驱体溶液，第二原料液为水溶液。前驱体溶液为85％磷酸、2.5mol/L LiOH水溶液和1.0mol/L FeSO4水溶液按照一定加料顺利配置而成的悬浊液，经过XRD分析可知沉淀物相为Li3PO4和Fe3(PO4)2·8H2O，悬浊液的pH值为6.2，温度为60℃。经预热器5的预热水的出口温度为200℃，前驱体溶液与预热水的体积比例为1∶10，管径为DN25，前驱体流量为160L/h，水的流量为1600L/h。第一结晶器6的管内流速为1.0m/s，停留时间为5min，第一结晶器6的管道布置采用卧式U型排列，管道总长为300m，维持管内温度为187℃，第二结晶器7温度为175℃，第二结晶器7的停留时间为2.5h，LiFePO4的等电点约为3.55，第二结晶器7内悬浮晶浆的pH值控制为6.8，远离等电点，避免颗粒聚集生长，出料阀14的控制压力为0.9MPa，冷凝器12出口温度为50℃，过滤器13的滤网为1.0μm。所制备的的亚微米级磷酸铁锂的产品粒径D50＝325.6nm，PDI＝0.135，D97＝397nm。
以上所述的仅是本发明的一些实施方式。对于本领域的普通技术人员来说，在不脱离本发明创造构思的前提下，还可以做出若干变形和改进，这些都属于本发明的保护范围。

Claims (10)

  1. 连续化水热法制备亚微米材料的装置系统，其特征在于，包括第一配料釜(1)、第二配料釜(2)、预热器(5)、第一结晶器(6)、第二结晶器(7)和换热器(9)；
    所述第一配料釜(1)通过管线依次连通第一进料泵(2)和预热器(5)，所述第二配料釜(2)通过管线连通第二进料泵(4)，所述预热器(5)和所述第二进料泵(4)均通过管线连通所述第一结晶器(6)的入料口；
    所述第一结晶器(6)的出料口通过管线连通所述第二结晶器(7)的入料口，所述第二结晶器(7)的出料口通过管线连通所述换热器(9)的入口，所述换热器(9)的出口分为两个，所述换热器的一个出口连通外循环单元再连通所述第二结晶器(7)的入口，所述换热器的另一个出口连通后处理单元再连通所述料浆收集器(15)；
    其中，所述第一结晶器(6)为管式反应结晶器，所述第二结晶器(7)为连续型反应结晶器。
  2. 根据权利要求1所述的连续化水热法制备亚微米材料的装置系统，其特征在于，所述第二结晶器(7)为DTB型结晶器。
  3. 根据权利要求1所述的连续化水热法制备亚微米材料的装置系统，其特征在于，所述管式反应结晶器为由多段具有相同内径的管道混合器组成，所述管式反应结晶器的管径为DN25～DN125mm。
  4. 根据权利要求1或2或3所述的连续化水热法制备亚微米材料的装置系统，其特征在于，所述外循环单元包括循环泵(10)；所述后处理单元包括依次连通的冷凝器(12)、过滤器(13)和出料阀(14)。
  5. 根据权利要求4所述的连续化水热法制备亚微米材料的装置系统，其特征在于，所述外循环单元还包括水力超声发生器(11)，所述水力超声发生器(11)设于所述循环泵(10)与所述第二结晶器 (7)之间；所述出料阀(14)为背压阀。
  6. 根据权利要求5所述的连续化水热法制备亚微米材料的装置系统，其特征在于，所述第一进料泵(3)、第二进料泵(4)和循环泵(10)的附近均设有流量计，所述第二结晶器(7)的外循环的管线上设有pH检测仪以及pH值进料液调节阀(8)。
  7. 基于权利要求4至6任一项所述的连续化水热法制备亚微米材料的装置系统的连续化水热法制备亚微米材料的制备工艺，其特征在于，该工艺包括如下步骤：
    盛装于第一配料釜(1)的第一原料液经第一进料泵(3)输送后进入预热器(5)预热至一定温度，盛装于第二配料釜(2)的第二原料液经第二进料泵(4)输送并与经预热后的第一原料液按一定体积比例进入第一结晶器(6)，得到料浆，料浆在第一结晶器(6)中以一定的流速流动一段时间后，进入第二结晶器(7)；
    料浆进入第二结晶器(7)进行晶化，部分料浆从第二结晶器(7)的出料口流出，经换热器(9)换热，在循环泵(10)的驱动下并与来自第一结晶器(6)的料浆混合后再次进入第二结晶器(7)，构成一个外循环，在第二结晶器(7)中反应一段时间后，得到悬浮晶浆；
    悬浮晶浆从第二结晶器(7)的出料口流出，经过换热器(9)换热，冷凝器(12)冷凝至一定温度后，通过过滤器(13)过滤，得到粒度均一化的晶浆，在出料阀(14)的作用下，晶浆稳定出料并收集于料浆收集器(15)；
    其中，所述第一原料液为前驱体溶液，所述第二原料液为水溶液或另一前驱体溶液；在晶化过程中，调控所述第二结晶器(7)中的晶浆的pH以控制悬浮晶体表面的Zeta电位，通过控制流速和反应时间来控制悬浮密度，避免晶浆的颗粒聚集生长。
  8. 根据权利要求7所述的连续化水热法制备亚微米材料的制备工艺，其特征在于，所述第一原料液经所述预热器(5)的预热温度为100～350℃。
  9. 根据权利要求7所述的连续化水热法制备亚微米材料的制备工艺，其特征在于，所述第二原料液与预热后的第一原料液按1∶1～1∶10的体积比例进入所述第一结晶器(6)。
  10. 根据权利要求7所述的连续化水热法制备亚微米材料的制备工艺，其特征在于，料浆在所述第一结晶管(6)管内的流速为0.25～1.0m/s，停留时间为1～30min；在所述第二结晶器(7)的反应时间为0.5～24h，所述经冷凝器(12)后的温度为25～60℃；所述过滤器(13)的滤网精度为1.0μm。
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