WO2000059599A1 - Reacteur a champ supergravitationnel de type courant de foucault - Google Patents

Reacteur a champ supergravitationnel de type courant de foucault Download PDF

Info

Publication number
WO2000059599A1
WO2000059599A1 PCT/CN1999/000114 CN9900114W WO0059599A1 WO 2000059599 A1 WO2000059599 A1 WO 2000059599A1 CN 9900114 W CN9900114 W CN 9900114W WO 0059599 A1 WO0059599 A1 WO 0059599A1
Authority
WO
WIPO (PCT)
Prior art keywords
liquid
vortex
reaction
chamber
reaction chamber
Prior art date
Application number
PCT/CN1999/000114
Other languages
English (en)
Chinese (zh)
Inventor
Xiaojun Pan
Wuyi Wang
Original Assignee
Xiaojun Pan
Wuyi Wang
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CN 99208429 external-priority patent/CN2382463Y/zh
Priority claimed from CN99105437A external-priority patent/CN1098728C/zh
Application filed by Xiaojun Pan, Wuyi Wang filed Critical Xiaojun Pan
Priority to AU52771/99A priority Critical patent/AU5277199A/en
Publication of WO2000059599A1 publication Critical patent/WO2000059599A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1806—Stationary reactors having moving elements inside resulting in a turbulent flow of the reactants, such as in centrifugal-type reactors, or having a high Reynolds-number

Definitions

  • the invention relates to a eddy current type super-gravity field reaction device used for enhanced transmission in chemical production or waste product purification process, particularly for a transmission reaction process including a two-phase or multi-phase system.
  • a eddy current type super-gravity field reaction device used for enhanced transmission in chemical production or waste product purification process, particularly for a transmission reaction process including a two-phase or multi-phase system.
  • the effect of interphase transfer and reaction effects are related to factors such as the physical and chemical properties of the vapor-liquid solid phase, humidity, and pressure, as well as the size of the contact area between phases, flow conditions, and relative speed. .
  • traditional equipment such as packed towers, plate towers, and reticulated membrane towers, etc.
  • the liquid phase flows naturally from top to bottom by gravity, so the liquid film thickness, low flow rate, and long residence time.
  • Mass processes and selective absorption are very unfavorable. Due to the limitation of buoyancy factors, the gas velocity at the flooding point is relatively low for the gas phase. This is also disadvantageous for strengthening the gas phase control mass transfer process and reducing equipment volume.
  • a rotating packed bed (referred to as an overweight machine). It is a kind of equipment that uses centrifugal force to strengthen the transmission and mixing process.
  • the typical structure of this type of equipment is composed of a sealed casing and a high-speed rotating annular packed bed.
  • a liquid distributor is set in the middle of the annular packing layer of the rotor. From the inner ring of the filler to the filler, the side of the casing is provided with air inlet holes. Under the effect of the pressure gradient, the gas enters the filling layer from the outer ring of the filler in a ring shape, and the vapor and liquid phases contact in the filler.
  • This type of equipment can generate a stable and adjustable centrifugal force field during operation, which improves the buoyancy factor by 1 to 3 orders of magnitude.
  • Liquids are subject to large shear forces in the supergravity field. As a result, it is pulled into a very thin film, very thin filaments and tiny drops, and the surface is quickly renewed, resulting in a huge phase-to-phase contact area, thus greatly increasing the mass transfer rate and also increasing the pan-point gas velocity. All of this is very beneficial to the enhanced mass transfer process, and can greatly reduce the equipment volume and investment. Because of its excellent characteristics, it solves many problems that are difficult to solve under the normal gravity field. Therefore, it has achieved outstanding results in applications such as absorption, analysis, and distillation.
  • the purpose of the present invention is to provide a vortex-type hypergravity field reaction device, which can move statically to completely solve the problems due to mechanical movement; make full use of the characteristics of rotating fluid to further improve the reaction efficiency; and can be applied to multi-phase A device in which a stream participates in a reaction in a hypergravity field.
  • a vortex-type hypergravity field reaction device is characterized in that it is provided with at least one reaction chamber, and a continuous phase inlet is provided on the reaction chamber; a fixed support is provided in the reaction chamber, and the support is provided on the support A carrier capable of attaching a reactant is arranged on the continuous phase inlet and the carrier is arranged tangentially; a liquid distributor is provided at the corresponding position of the reaction chamber and the carrier; a separation chamber is connected to the rear of the last-stage reaction chamber, and the continuous The phase outlets are provided in the separation chambers; each room is separated by a partition plate, and is communicated with each other through the gap of the partition plate; a liquid collecting tank and a discharge port are arranged at the lower part of the device.
  • the carrier provided on the above-mentioned support body may be a reticulum, which may be vortex-shaped, sheet-shaped, or multilayer composite, or may be ring-shaped, star-shaped, spiral-shaped, or wing-shaped.
  • the support may be a honeycomb packing or a packed bed.
  • the continuous phase inlet is convergent, and a gap adjustment device is provided in the continuous phase inlet.
  • Two or more reaction chambers can be connected in series, separated by a partition, and communicated by a gap around the partition.
  • a liquid collecting tank can be provided at the lower end of the reaction chamber, and a draining space is provided between the liquid collecting tank and the reaction chamber. Seam.
  • the liquid collecting tank may also be provided at the lower end of the separation chamber, and a liquid discharge slit is provided between the liquid collecting tank and the separation chamber.
  • the reaction chamber can be arranged above and below in series, and a partition plate is provided between the two reaction chambers, which can communicate with each other through the through holes on the partition.
  • the separation chamber can be set at the upper end of the upper reaction chamber, and the continuous phase outlet can be set at the separation.
  • a liquid distributor is provided at the upper end of the carrier to which the reactant is attached on the support.
  • This device can be used in absorption, adsorption, disintegration, distillation, drying, catalytic conversion, liquid-liquid extraction, exhaust gas purification and dust removal processes in petroleum, chemical, metallurgy, pharmaceutical, food and environmental protection industries, and viscosity values less than 10 poise In the preparation process of the substance.
  • the working principle of the present invention is that the basic main structure of the present invention is a device including a continuous phase inlet, a liquid distributor, a reaction chamber, a separation chamber, and a continuous phase outlet, and a liquid collecting tank and a discharge port are arranged at the lower part of the device;
  • the reaction chamber is provided with a fixed support, and a support capable of attaching reactants, such as a hollow vortex grid or a packed bed, is arranged on the support.
  • the continuous phase inlet and the support are tangentially arranged.
  • the reaction chamber is separated from the support.
  • the room is separated by a partition.
  • the air flow is introduced from the continuous phase inlet placed tangentially on the side of the reaction chamber, and it rotates at high speed in the reaction chamber to form a stable hypergravity field, and its speed can be controlled by the wind pressure of the fan.
  • the continuous phase can be the reaction gas itself, or it can be used only as power.
  • the reaction liquid is uniformly sprayed from the liquid distributor to the grid to form a liquid film. Due to the high-speed cutting movement of the air flow, the surface of the reactant carrier is under pressure, and the liquid film is continuously thinned until it is shredded, atomized, and a particulate dispersion system is quickly formed.
  • the rotating fluid can be divided into two characteristic regions, a quasi-potential flow region and a solid-like region (or vortex core).
  • the fluid In the quasi-potential flow zone, the fluid has a laminar flow characteristic and is mainly dominated by a centrifugal separation mechanism. Large-particles are separated here.
  • the tangential velocity at the junction (transition zone) of the quasi-potential flow zone and the vortex core zone is the largest.
  • the speed of the fluid decreases sharply along the radius and approaches Q when it reaches the center.
  • the pressure approaches - ⁇ , and the particles are "inhaled” in a large amount.
  • the dust and mist droplets collide and pass through the transition area after the mass increases.
  • the device is changed to a peripheral outflow mode, and the above-mentioned characteristics of the rotating body are maintained and effectively utilized, resulting in a great improvement in the capture efficiency of particles and ensuring that the absorption and separation are completed in the device at one time.
  • the liquid was shaken by the centrifugation to the wall and flowed into the liquid storage tank.
  • the gas enters the separation chamber through the gap around the baffle, and is discharged or recovered after further dehumidification (also can be recycled). Liquid and solid are discharged from the discharge port in time.
  • the device has the following characteristics compared with the prior art:
  • the device is powered by a continuous phase.
  • the continuous phase used can be a gas or a liquid.
  • the continuous phase can participate in the reaction, or it can only serve as a motive force; it can be a single phase or a mixture of two or more.
  • the super-gravity field formed by the fan (or pump) and the control of the inlet opening degree is stable and reliable, and the speed can reach 10,000 rpm (the speed of existing super heavy machines is generally about 1-2 thousand rpm).
  • Speed regulation is free and easy, quick start and stop, and can be operated under positive pressure or negative pressure.
  • the hollow vortex grid moves statically. There is no mechanical operation problem. The rotating gas cuts with it multiple times. The relative speed is very high, which can atomize the liquid film on the net, continuously update the surface, and have a large contact area between phases. Mass transfer The coefficient is high.
  • the vortex grid can be designed to be hollow to avoid clogging. At the same time, the characteristics of the vortex core area and the separation effect of the transition area can be effectively used to improve the capture efficiency of particles.
  • the device has impact atomization, the requirements on the liquid distributor itself are not high, and the power consumption and corresponding wear of various atomizing nozzles (such as rotary atomizer and jet atomizer) are avoided. And clogging.
  • atomizing nozzles such as rotary atomizer and jet atomizer
  • Vortex can be made into various forms. Such as vortex packed bed, vortex plate, etc., can also be made into other shapes, such as ring, star, spiral, sheet, wing and other grids or packed beds.
  • the surface of the net, plate and filler can intervene with the catalyst.
  • the net frame is a whole, which is easy to disassemble, easy to maintain and replace, and can be applied to many different reaction occasions.
  • the reaction chamber can be designed as a multi-stage series, which can continuously complete different reactions (such as selective absorption). Can also be used in parallel to handle the reaction of a large number of materials.
  • FIG. 1 is a structural external view of a first embodiment of the present invention.
  • FIG. 1A is a side view of FIG. 1.
  • FIG. 1B is a top view of FIG. 1.
  • Fig. 2 is a sectional view taken along the line B-B in Fig. 1.
  • Fig. 3 is a cross-sectional view taken along A-A of Fig. 1C.
  • FIG. 4 is a schematic structural diagram of a second embodiment of the present invention.
  • FIG. 5 is a schematic structural diagram of a third embodiment of the present invention.
  • FIG. 6 is a schematic structural diagram of a fourth embodiment of the present invention.
  • FIG. 7 is a schematic structural diagram of a fifth embodiment of the present invention.
  • FIG. 8 is a schematic structural diagram of a hollow vortex network of the present invention.
  • Figure 9 Schematic diagram of the multilayer composite omentum in the present invention.
  • FIG. 10 is a schematic structural diagram of a spiral vortex network in the present invention.
  • FIG. 11 is a schematic structural diagram of an annular vortex network according to the present invention.
  • FIG. 12 is a schematic structural diagram of a star-shaped vortex network in the present invention.
  • FIG. 13 is a schematic structural diagram of a wing-shaped vortex net in the present invention. Way of carrying out the invention
  • At least one vortex-type hypergravity field reaction device of the present invention includes a continuous phase inlet 1, a liquid distributor 8, a reaction chamber 2, a separation chamber 3, and a continuous phase outlet 4.
  • the lower part is provided with a liquid collecting tank 6 and a discharge port 7;
  • a reaction carrier 1 is provided with a reactant carrier, and in this embodiment, the carrier is a hollow vortex net 11;
  • the reaction chamber 2 and the separation chamber 3 are separated by a baffle plate 9.
  • the hollow vortex net 11 is made as a separate body from the main body, which is easy to disassemble and facilitate maintenance, and can be used on the hollow vortex net 1 1 as required. Equipped with different omentum forms.
  • the continuous phase inlet 1 is a convergent inlet.
  • a conical continuous phase inlet 1 is provided with a wedge-shaped slider 1 3.
  • the wedge-shaped slider 1 3 can be moved up and down along the continuous phase inlet 1 to adjust the size of the opening gap of the continuous phase inlet 1.
  • the adjustment structure for the vertical movement of the wedge-shaped slider 1 3 is generally constituted by a conventional lifting adjustment mechanism (for example, a structure in which a slide rail is matched with a convex pin or a jack pushing structure) is not repeated here.
  • the hollow vortex network 11 is shown in FIG. 8. It comprises an inner and outer two-layer mesh support 12, and several arc-shaped omentum 14 are connected between the inner and outer two-layer mesh support 12 to form a hollow vortex network 11.
  • the hollow vortex net 11 is fixedly disposed in the reaction chamber 2.
  • the phase direction of the convergent continuous phase inlet 1 described above is tangent to the omentum 14 on the hollow vortex network 11.
  • a liquid collecting tank 6 is provided below the reaction chamber 2, and a liquid discharging slit 10 is provided between the reaction chamber 2 and the liquid collecting tank 6.
  • a discharge port 7 is provided below the header tank 6.
  • a separation chamber 3 is connected to the rear of the reaction chamber 2.
  • the reaction chamber 2 and the separation chamber 3 are separated by a partition plate 9.
  • the bottom end of the separation chamber 3 is provided with an annular groove and a drain port 5. Backmixing in liquid-solid separation.
  • the continuous phase outlet 4 is provided in the separation chamber 3.
  • the continuous phase is gas, that is, the boiler flue gas from the multi-tube dust collector.
  • the components to be purified and removed from the flue gas are fine dust and SO 2
  • the absorption liquid is a lime emulsion.
  • the smoke stream is tangentially introduced from the continuous phase inlet 1 and forms a high-speed vortex-like supergravity field in the reaction chamber 2.
  • the air flow and the hollow hollow vortex network 1 1 intersect multiple times, resulting in a high relative
  • the water film sprayed by the liquid dispenser 8 on the mesh film 14 is broken at a speed, so that a large and constantly updated contact surface area is obtained, and the water droplets are further evaporated and atomized due to the heat transfer of the smoke stream itself.
  • the contact surface is further increased, which effectively improves the absorption and transformation intensity of Ca 2+ and water for S0 2 and the capture efficiency of fine dust; the fine dust and water mist entering the vortex core area collide with each other and condense, and then again when entering the vortex water film web is intercepted, participation basic oxide contained in the dust after the dissolution of the absorption of S0 2, the absorbent liquid can reduce the amount of the basic substance, the amount of circulating liquid is reduced. After the reaction is completed, the liquid and the dust particles entrained by the liquid return to the wall of the device by centrifugal action, flow into the collecting tank 6 from the slot 10, and are controlled to be discharged through the discharge port 7.
  • the purified gas passes around the baffle 9
  • the gap enters the separation chamber 3 and is dehumidified.
  • the liquid is forced into the annular groove at the bottom by the airflow and flows out from the liquid discharge port 5.
  • the gas is returned along the outer wall of the continuous phase outlet 4 into the continuous outlet 4 and discharged.
  • Another specific application example of this embodiment is a preparation process in which the viscosity of the product is relatively low.
  • the CO 2 gas is introduced from the continuous phase inlet 1 placed at the side of the reaction chamber 2 in a tangential position, and rotates at a high speed in the reaction chamber 2 to form a stable hypergravity field. Its rotation speed can be controlled by wind pressure and wedge-shaped sliders 13 located in the inlet.
  • the reaction liquid is sprayed uniformly by the liquid distributor 8 to the grid to form a liquid film. Due to the cutting action of the air stream, a particulate dispersion system is formed in the vapor and liquid of the omentum, which creates sufficient conditions for the vapor-liquid-liquid three-phase material transfer reaction. After the reaction is complete. Liquid substances and particles are thrown to the wall due to centrifugal force and collected by the collecting tank 6.
  • Fig. 4 shows the structure of a second embodiment of the present invention.
  • this embodiment there are two reaction chambers 2 of the same structure that are connected side by side in series.
  • the structure of the two reaction chambers 2 is exactly the same as that of the first embodiment.
  • the two reaction chambers 2 are separated by a partition plate 9, and the two reaction chambers 2 are connected to form a two-stage series by using a gap around the partition plate 9.
  • the structure of this embodiment can be applied to a multi-stage absorption process. It works as follows:
  • the first stage uses a high-concentration ammonium sulfite solution to absorb SO 2 in the tail gas of the sulfuric acid process, so as to ensure the concentration requirements of the by-product ammonium sulfite.
  • the remaining SO 2 is further absorbed in the second stage with a lower concentration solution to ensure that the SO 2 content in the exhaust gas meets the emission standard.
  • concentration of the absorption liquid at the latter pole is increased to a certain degree, it is used in the first stage. This can replace two industrial towers. And there is no problem of secondary pollution.
  • FIG. 5 shows a third embodiment of the present invention.
  • it includes an aversion chamber 2 in which a hollow vortex net 11 is fixed, and a liquid distributor 8 is provided at the center of the hollow vortex net 11.
  • a continuous phase inlet 1 is provided at the upper end of the reaction chamber 2 slightly offset from the axial center of the hollow vortex net 11.
  • An axially elongated separation chamber 3 is connected to the rear of the reaction chamber 1. The two chambers are separated by a partition plate 9 and are connected to each other by a gap around the partition plate 9.
  • the continuous phase outlet 4 is provided in the separation chamber 3, and a liquid discharge slit 10 is provided at the lower part of the separation chamber 3 and communicates with a liquid collecting tank 6.
  • a discharge port 7 is provided at the lower end of the collecting tank 6; the grid frame 11 and the main system are composed of components, and the net membrane 14 is in the form of dense inner and thin outer layers, which can effectively control the generation of droplets.
  • the structure of this embodiment is mainly applied to liquid-liquid extraction.
  • the existing extraction tower has an effective height of about 60%-90% to compensate for the adverse effects caused by the vertical mixing effect.
  • the flow rate of the raw material liquid and the extractant passing through the extraction tower in a unit time cannot be Increase arbitrarily, otherwise flooding will occur.
  • the use of Bode and Lowell centrifugal extractors can significantly reduce equipment size and increase productivity. But similar to super heavy machines, this type of equipment requires large power consumption and faces more complicated mechanical maintenance problems.
  • the separation chamber is lengthened on the basis of the basic main structure and the liquid collection tank is placed at the end of the separation chamber.
  • the light liquid is used as the continuous phase, and the heavy liquid is added by the liquid distributor.
  • the two phases are in reverse contact (due to the large viscosity of the heavy liquid, the retention of the vortex can prevent it from forming droplets, thereby preventing emulsification), and disperse.
  • the heavy liquid droplets gradually moved towards the outer edge of the reactor due to centrifugation. After the reaction, the two liquids entered the separation chamber at the same time. After layering, the light liquid was discharged from the continuous phase outlet, and the heavy liquid was discharged into the collection tank and controlled by the discharge port.
  • Fig. 6 shows a fourth embodiment of the present invention.
  • a grid frame 11 is provided in each reaction chamber 2.
  • a continuous phase inlet 1 is provided in a horizontal direction where the grid frame 11 is tangent.
  • Two reaction chambers are provided. Two are separated by a partition plate 9, and through holes 91 are distributed on the partition plate 9; a lower end of the lower reaction chamber 2 is provided with a liquid collecting tank 6 separated by the partition plate 9, and the partition plate 9 here may be provided in a cone shape.
  • the holes in the periphery and the center of the partition plate 9 communicate with the lower reaction chamber 2.
  • the upper part of the upper reaction chamber 2 is connected to a separation chamber 3, and the two chambers are also separated by a partition plate 9 and are connected by the periphery of the partition plate 9.
  • the continuous phase outlet 4 is provided at the upper end of the separation chamber 3.
  • the liquid distributor 8 is provided on the upper part of the upper reaction chamber.
  • This embodiment is applied to an evaporative concentration process.
  • a multi-effect evaporator to concentrate the dilute black liquor before spraying it into a combustion furnace to burn off organic matter. This process has a long process and large thermal energy loss.
  • the flue gas can enter tangentially in sections, and the black liquid is sprayed in by the top annular liquid distributor 8
  • the hollow vortex net 11 and the mesh membrane 14 adopt a multi-layer composite type as shown in FIG. 9 to increase the liquid carrying capacity. Compared with the existing hollow body DC spray drying tower, the efficiency is greatly improved.
  • the present invention Since the present invention has extremely strong dispersibility for liquids and a certain liquid-holding capacity, and can keep the hot smoke stream in the device for a longer residence time, the heat energy utilization rate is high. Therefore, the black liquor can be concentrated or even evaporated by using the flue gas from a paper mill's own boiler or directly from the combustion furnace flue gas. At the same time, the coal dust and S0 2 in the flue gas can be efficiently removed, and good economic benefits and the environment have been received. benefit.
  • Fig. 7 shows a fifth embodiment of the present invention.
  • the structure shown in this embodiment can be applied to catalytic combustion.
  • the catalytic combustion method can be used to reduce the light-off temperature to 523 to 623K, and the residence time is shortened to 0.005-0.011 s.
  • This embodiment can constitute a combustion chamber in a combustion purification system for organic waste gas. As shown in FIG. 7, it includes a reaction chamber 2.
  • the organic phase is used for the continuous phase, and it enters from the continuous phase inlet 1 at a high speed.
  • a hollow vortex net 1 1 is provided.
  • the hollow vortex net 11 may be a metal net having a structure as shown in FIG.
  • FIG. 10 to FIG. 13 show different structures of the vortex net of the present invention, and users can choose according to different usage requirements.
  • a spiral vortex net 15 shown in FIG. 10 has no hollow core, so it is often used in a structure where the liquid distributor 8 is provided at the upper end of the reaction chamber 2, as shown in FIG. 6 Structure;
  • FIG. 11 shows an annular vortex network 16, which can increase the penetration time of two-phase reactants, In this way, the reaction time in the reaction chamber 2 is increased;
  • FIG. 12 shows a star-shaped vortex network 17, each plate 171 of the star-shaped vortex network 17 is composed of a mesh film 172 on the upper and lower layers, in two layers
  • a honeycomb filler 173 can be sandwiched between the reticles 172;
  • FIG. 13 shows a winged vortex 18, and the reticular vortex 18 has a curved wing 182 on the reticular 181.
  • This structure can increase The surface area of the omentum 181 increases the reactant's ability to

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un réacteur à champ supergravitationnel de type courant de Foucault caractérisé en ce qu'il comprend au moins une chambre de réaction au-dessus de laquelle est ménagée une entrée d'alimentation en continu et dans laquelle est fixé une structure sur laquelle repose un support auquel le réactant peut adhérer, l'entrée et le support se coupant ; un distributeur de liquide relié à la partie faisant face à la chambre de réaction; une chambre de séparation reliée à la partie arrière de la dernière chambre de réaction, une sortie en continu ménagée dans la chambre de séparation ; une chicane venant entre chaque chambre; des moyens de collecte de liquide et une ouverture de décharge ménagée au fond du réacteur. L'invention peut être utilisée dans un processus de réaction consistant à effectuer un transfert entre deux ou plusieurs phases, notamment une réaction physique et chimique entre les phases gaz-liquide, liquide-liquide ou gaz-liquide-solide.
PCT/CN1999/000114 1999-03-31 1999-08-12 Reacteur a champ supergravitationnel de type courant de foucault WO2000059599A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU52771/99A AU5277199A (en) 1999-03-31 1999-08-12 Supergravitational field vortex reactor and the use thereof

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN 99208429 CN2382463Y (zh) 1999-03-31 1999-03-31 气动涡流式超重力场反应装置
CN99208429.6 1999-03-31
CN99105437.7 1999-04-06
CN99105437A CN1098728C (zh) 1999-04-06 1999-04-06 涡流式超重力场反应装置及其应用

Publications (1)

Publication Number Publication Date
WO2000059599A1 true WO2000059599A1 (fr) 2000-10-12

Family

ID=25745011

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN1999/000114 WO2000059599A1 (fr) 1999-03-31 1999-08-12 Reacteur a champ supergravitationnel de type courant de foucault

Country Status (2)

Country Link
AU (1) AU5277199A (fr)
WO (1) WO2000059599A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004050232A1 (fr) * 2002-12-03 2004-06-17 Process Kinetics Limited Reacteur centrifuge a commande de temps de sejour
CN111530384A (zh) * 2020-04-02 2020-08-14 北京化工大学 气液反应及旋转除沫一体化超重力装置、气液反应系统
CN112547072A (zh) * 2019-09-10 2021-03-26 中国石油化工股份有限公司 负载型催化剂和应用以及制备低级脂肪胺的方法
CN113769684A (zh) * 2021-08-24 2021-12-10 北京化工大学 用于液-液非均相反应及产物两相分离过程高效耦合强化的超重力装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105854332B (zh) * 2016-05-18 2018-12-11 中北大学 复合式多级旋转填料床传质反应装置及其完成的反应方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4382900A (en) * 1980-09-01 1983-05-10 Imperial Chemical Industries Plc Centrifugal gas-liquid contact apparatus
CN1059105A (zh) * 1991-10-08 1992-03-04 北京化工学院 旋转床超重力场强化传递与反应装置
CN2102788U (zh) * 1991-10-25 1992-04-29 李诗英 带阻排液装置的超重力场卧式旋转床
CN2229833Y (zh) * 1995-06-13 1996-06-26 华南理工大学 同心圆环薄板填料旋转床气液传质反应器

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4382900A (en) * 1980-09-01 1983-05-10 Imperial Chemical Industries Plc Centrifugal gas-liquid contact apparatus
CN1059105A (zh) * 1991-10-08 1992-03-04 北京化工学院 旋转床超重力场强化传递与反应装置
CN2102788U (zh) * 1991-10-25 1992-04-29 李诗英 带阻排液装置的超重力场卧式旋转床
CN2229833Y (zh) * 1995-06-13 1996-06-26 华南理工大学 同心圆环薄板填料旋转床气液传质反应器

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004050232A1 (fr) * 2002-12-03 2004-06-17 Process Kinetics Limited Reacteur centrifuge a commande de temps de sejour
CN112547072A (zh) * 2019-09-10 2021-03-26 中国石油化工股份有限公司 负载型催化剂和应用以及制备低级脂肪胺的方法
CN112547072B (zh) * 2019-09-10 2023-08-15 中国石油化工股份有限公司 负载型催化剂和应用以及制备低级脂肪胺的方法
CN111530384A (zh) * 2020-04-02 2020-08-14 北京化工大学 气液反应及旋转除沫一体化超重力装置、气液反应系统
CN113769684A (zh) * 2021-08-24 2021-12-10 北京化工大学 用于液-液非均相反应及产物两相分离过程高效耦合强化的超重力装置

Also Published As

Publication number Publication date
AU5277199A (en) 2000-10-23

Similar Documents

Publication Publication Date Title
EP3202483B1 (fr) Système intégré de couplage d'écoulement rotationnel et d'écoulement plongeant pour la désulfuration et le dépoussiérage ultra-propres et procédé de désulfuration et de dépoussiérage s'y rapportant
US4963329A (en) Gas reacting apparatus and method
CN202569944U (zh) 旋流气动涡流脱硫乳化器和文丘里管涡流乳化脱硫塔
CN102657991B (zh) 一体化文丘里空气洗涤装置
US5023064A (en) Method for removing sulfur oxide
WO2006128351A1 (fr) Colonne a garnissage reflechissante
CN103301958B (zh) 气液分离装置
CN207661867U (zh) 空气净化器
CN101690867B (zh) 一种半干式循环流化床切流与直流复合进气脱硫塔
CN105107355B (zh) 吸收分离一体化含硫气体脱硫旋流反应装置
WO2000059599A1 (fr) Reacteur a champ supergravitationnel de type courant de foucault
CN113797672B (zh) 用于从废气中去除颗粒的气体清洗器和废气处理设备
CN105289861B (zh) 一种旋风分离器
WO2005035103A1 (fr) Tour de desulfuration a sec des gaz de combustion
CN106000013A (zh) 湿法脱硫烟气超净排放处理系统
RU2344869C2 (ru) Способ сепарации жидкости из газового потока и устройство для его осуществления
CN2382463Y (zh) 气动涡流式超重力场反应装置
CN109420385A (zh) 一种涡式空气净化器及基于该净化器的空气净化方法
CN209060564U (zh) 一种低温scr催化剂粉体的喷雾干燥生产设备
CN1221644A (zh) 旋流离散吸收分离方法与吸收塔
CN1098728C (zh) 涡流式超重力场反应装置及其应用
CN100425312C (zh) 一种组合式喷雾蒸发浓缩干燥的方法及设备
CN214701468U (zh) 一种喷雾干燥设备
CN209173731U (zh) 一种新型高效喷淋气动乳化脱硫、除尘装置
CN211487045U (zh) 一种拉幅定型机废气分离净化设备

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CU CZ DE DK EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW SD SL SZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
NENP Non-entry into the national phase

Ref country code: CA

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

122 Ep: pct application non-entry in european phase