WO2013022126A1 - Appareil et procédé d'accélération de réaction en phase hétérogène pour un fluide - Google Patents

Appareil et procédé d'accélération de réaction en phase hétérogène pour un fluide Download PDF

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Publication number
WO2013022126A1
WO2013022126A1 PCT/KR2011/005757 KR2011005757W WO2013022126A1 WO 2013022126 A1 WO2013022126 A1 WO 2013022126A1 KR 2011005757 W KR2011005757 W KR 2011005757W WO 2013022126 A1 WO2013022126 A1 WO 2013022126A1
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WO
WIPO (PCT)
Prior art keywords
fluid
reaction tube
reaction
mixed
discharge pipe
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Application number
PCT/KR2011/005757
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English (en)
Korean (ko)
Inventor
문광순
윤승규
Original Assignee
재단법인 한국계면공학연구소
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Priority to KR1020147006169A priority Critical patent/KR101580583B1/ko
Priority to PCT/KR2011/005757 priority patent/WO2013022126A1/fr
Publication of WO2013022126A1 publication Critical patent/WO2013022126A1/fr

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    • 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
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • 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
    • B01J19/0053—Details of the reactor
    • B01J19/006—Baffles
    • 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
    • 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/03—Preparation of carboxylic acid esters by reacting an ester group with a hydroxy group
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
    • C11C3/10—Ester interchange

Definitions

  • the present invention relates to a reaction promoting device for non-homogeneous fluids and a method for promoting a reaction of non-homogeneous fluids that promote the reaction of non-homogeneous fluids that do not dissolve together.
  • a phase is a critical phase such as a solid phase, a liquid phase, a gas phase, or a plasma, depending on the state of a substance, and is divided into a homogeneous phase and a heterogeneous phase according to whether two phases have the same phase.
  • a critical phase such as a solid phase, a liquid phase, a gas phase, or a plasma, depending on the state of a substance, and is divided into a homogeneous phase and a heterogeneous phase according to whether two phases have the same phase.
  • hydrophilicity liquids that mix well with water and hydrophobisity liquids that do not mix well with water can be regarded as non-homogeneous fluids.
  • the present invention is to provide a reaction promoting device and a reaction promoting method for promoting the reaction rate of a non-homogeneous liquid having very low reactivity since they are not dissolved in each other. To this end, the present invention focuses on the interface of the non-homogeneous fluid and provides a means for greatly accelerating the reaction rate of the non-homogeneous fluid.
  • the reaction promotion apparatus of the non-homogeneous fluid of the present invention includes a reaction tube in which the first fluid is accommodated to produce a mixed fluid by ester reaction of a first fluid and a second fluid, and the reaction. And a spraying unit provided with a nozzle extending the interface of the second fluid by injecting the second fluid into fine particles inside the tube.
  • the mixed fluid production method by driving the pump to supply a first fluid to the supply, the heater to heat the first fluid, the reaction tube with the first fluid supplied through the supply And spraying the second fluid into the reaction tube with fine particles through a nozzle installed inside the reaction tube, and interfacial expansion effect due to an increase in the specific surface area of the fine particles, and suppresses the occurrence of fatty acid metal salts in the reaction tube.
  • the mixed fluid production method by driving the pump to supply a first fluid to the supply, the heater to heat the first fluid, the reaction tube with the first fluid supplied through the supply Of the fine particles to spray the second fluid into the reaction tube through the nozzles installed inside the reaction tube, and to suppress the interface expansion effect by the fine particles and the generation of fatty acid metal salts in the reaction tube.
  • At least one of an effect, a chemical effect by heating the first fluid, and a physical mixing effect by turbulent flow inside the reaction tube causes a transesterification reaction inside the reaction tube at a desired reaction rate, and a mixed fluid is produced.
  • the mixed fluid inside the reaction tube is supplied to the inline mixer of the mixer unit, and the inline mixer is rotated by external power.
  • a mixed reaction product of a hydrophobic substance and a hydrophilic substance can be produced in a short time and with high efficiency by injecting a second fluid into the first fluid supplied into the reaction tube with a nozzle.
  • the interfacial expansion effect due to the increase of the specific surface area of the fine particles, the effect of the fine particles to suppress the generation of fatty acid metal salt in the reaction tube, the chemical effect by the first fluid heating, the turbulent flow inside the reaction tube or physical mixing by the mixer unit At least one of the effects has the advantage that the transesterification reaction proceeds at the desired optimum reaction rate.
  • FIG. 2 shows one embodiment of the reaction promotion apparatus of the non-homogeneous fluid of the present invention which improves the reaction rate and the reaction yield by expanding the surface area of the interface by fine particle spraying.
  • FIG. 3 shows an embodiment in which the embodiment of FIG. 2 is optimized for mass production.
  • FIG. 4 to 6 are photographs taken inside the reaction tube.
  • FIG. 4 shows before injection
  • FIG. 5 immediately after injection
  • FIG. 6 shows a maximum injection state.
  • Representative non-homogeneous fluids for the purposes of the present invention include oil and methoxide.
  • Oil and methoxide are transesterified to biodiesel, and the mixed fluid of oil and methoxide becomes biodiesel.
  • a mixed fluid is prepared through a transesterification reaction in which glycerol is separated using methanol from triglycerides in which glycerol is bound to trivalent fatty acids, and then produced fatty acid esters.
  • factors affecting the reaction rate of a chemical reaction include, for example, the physicochemical properties of the reactants, concentration, temperature, pressure, catalyst, and the ability of the reactants to contact each other. Maximizing the contact area between the reactants among the factors affecting the chemical reaction rate is a common requirement in all chemical reactions, and maximizes the contact area at the interface between the reactants and the retention time through the contact. Is an important factor in determining reaction rate and reaction yield.
  • a phase is a critical phase such as a solid phase, a liquid phase, a gas phase, or a plasma depending on the state of a substance.
  • a phase has the same properties as a polar fluid such as water and ethanol, it can be regarded as a homogeneous phase fluid. Since they do not mix with each other like methanol, they can be regarded as heterogeneous phase fluids if they have different properties.
  • Homogeneous fluids are easily dissolved or mixed with each other so that no interface exists. For example, if a container is filled with water and ethanol is added to it, water and ethanol are easily mixed with the same polarity so that no distinct interface is formed.
  • non-homogeneous fluids do not dissolve or mix with each other, so there is a distinct interface due to the difference in density.
  • filling the vessel with oil and adding methanol to it does not easily mix the oil and the methanol with different polarities, so that the distinction between the bottom and the top of the vessel results in distinct densities, depending on the density difference.
  • non-homogeneous fluids can occur only at the interface, and if no interface exists or two non-homogeneous fluids are isolated from each other at the interface location, the chemical reaction of the non-homogeneous fluid cannot occur.
  • Reactions generally called two-phase reactions, refer to the reaction of two reactants with different phases of matter, such as solid-liquid and gas-liquid reactions.
  • a reactant having a hydrophobisity group and a reactant having a hydrophilicity group do not mix well with each other, as in the transesterification reaction, they are reactions between the same liquid state but a heterogeneous phase fluid, so it is like a two-phase reaction. It can be seen that the reaction proceeds. In this case, the reaction rate drops significantly.
  • Biodiesel is a mixed fluid by alcohol decomposition in which alcohol is added to triglyceride which is a main component of fats and oils. Biodiesel is prepared through transesterfication of alcohols and fats and oils using base or acid catalysts.
  • the main raw material of the biodiesel animal or vegetable oils and oils and fats and oils maintain the hydrophobic group of the triglyceride (triglyceride) and the alcohol in general has a hydrophilic group, the oil and alcohol are not easily dissolved at room temperature, atmospheric pressure.
  • the present invention is to increase the reaction rate and the reaction yield by injecting triglyceride or methanol as fine particles having a size of several to several tens of micrometers as a non-homogeneous fluid, thereby increasing the reaction area of the interface formed by the non-homogeneous fluid. It features.
  • reaction rate of the transesterification reaction by spraying a non-homogeneous fluid including triglyceride corresponding to the first fluid or methanol or methoxide corresponding to the second fluid in a mist state using the nozzle 120 inside the reaction tube and
  • the reaction yield can be increased.
  • reaction promoting device for a non-homogeneous fluid will be described taking a biodiesel production device as an example.
  • one of the 'mixed fluids' is biodiesel
  • one of the 'first fluids' is triglyceride
  • one of the 'second fluids' is methanol or methoxide.
  • Methoxide refers to a mixture of methanol and a catalyst (eg caustic soda).
  • FIG. 2 shows one embodiment of the reaction promotion apparatus of the non-homogeneous fluid of the present invention which improves the reaction rate and the reaction yield by expanding the surface area of the interface by fine particle spraying.
  • FIG. 3 shows an embodiment in which the embodiment of FIG. 2 is optimized for mass production. 2 and 3 are the same in their fundamental operating principle, so they will be described together.
  • the apparatus for promoting reaction of a non-homogeneous fluid of the present invention includes a reaction tube 110 for increasing a transesterification reaction rate by interfacial expansion by spraying fine particles of a nozzle 120. It may further include a mixer unit 200 for increasing the rate of transesterification by physical mixing.
  • the reaction unit 100 includes a reaction tube 110, a fixing plate 111, a fixing rod 112, a nozzle 120, a first discharge pipe 190, and a first valve 195. .
  • the second fluid supplied through the second fluid supply part 320 is injected into the fine particles by the nozzle 120.
  • the nozzle 120 injects the second fluid into the reaction tube 110 at a predetermined injection angle ⁇ .
  • the length L and the diameter D of the reaction tube 110 are constant levels depending on the injection angle ⁇ of the nozzle 120, the injection pressure, the size of the fine particles, and the diameter of the reaction tube 110 inlet and outlet. It is optimized to obtain the above transesterification rate.
  • both ends of the reaction tube 110 may be fixed to a plate to stably support the reaction tube 110. 111) is sandwiched between and supported.
  • the fixing plate 111 is coupled by the fixing rod 112 and the fixing plate 111 and the reaction tube 110 are firmly coupled by the tensile force of the fixing rod 112.
  • the first fluid is accommodated in the reaction tube 110.
  • the reaction rate is accelerated by the interface expansion effect because the second fluid is injected in the atomized or automized phase state.
  • fine particles of methanol or methoxide which is a second fluid
  • oil which is the first fluid
  • esterification reaction rate is dramatically increased according to the interfacial engineering physicochemical effect by the fine particle injection, the physical effect by the injection force of the nozzle 120, and the chemical effect by the temperature heating of the heater 390.
  • a supply part 310 for supplying a first fluid is connected to an inlet side of the reaction tube 110, and the first fluid is supplied with a supply pressure by the pump 380.
  • the outlet side of the reaction tube 110 is connected to the first discharge pipe 190 for discharging the mixed fluid inside the reaction tube 110.
  • the diameter of the reaction tube 110 is preferably larger than the diameter of the supply unit 310 and the first discharge tube 190.
  • the rate of transesterification reaction is increased. Due to the nature of the incompressible continuous fluid, the flow rate per unit time of the fluid is the same at the inlet and outlet of the reaction tube 110. Therefore, the reaction rate is increased when the fluid stays inside the large reaction tube 110 longer than the fluid stays in the small diameter supply unit 310 or the first discharge pipe 190. Since the second fluid injection angle of the nozzle 120, the diameter and the length of the reaction tube 110 are optimally designed, the transesterification reaction rate is enhanced.
  • the mixer unit 200 physically remixes the mixed fluid discharged from the reaction unit 100 to double the transesterification reaction rate, and includes an inline mixer 210.
  • the inline mixer 210 may have a blade that rotates by external power therein.
  • a zigzag static blade 212 is provided which triggers turbulent flow of the fluid by the shape feature in a fixed state, and another embodiment of the inline mixer 210 is provided. Yes.
  • a wing that is rotated by external power.
  • the first bypass pipe 201 is connected to the inlet side of the inline mixer 210 and the second discharge pipe 290 is connected to the outlet side.
  • the first bypass pipe 201 is connected to the first discharge pipe 190 corresponding to the outlet of the reaction unit 100.
  • the first valve 195 When the first valve 195 is opened, the mixed fluid supplied through the first discharge pipe 190 flows into the inlet side of the inline mixer 210 through the first bypass pipe 201.
  • the first valve 195 is closed, the mixed fluid is produced by the ester reaction by the reaction unit 100 alone without the action of the mixer unit 200.
  • the supply pressure of the first fluid, the supply flow rate of the first fluid, the supply temperature of the first fluid, the injection pressure of the second fluid, the injection flow rate of the second fluid, the injection angle of the second fluid, the fine particles of the second fluid The size, the length of the reaction tube 110, the diameter of the reaction tube 110 is determined according to the optimum response value according to various variables.
  • the method is not limited to one cycle of the reaction unit 100 and the mixer unit 200, and according to the method of repeatedly circulating the reaction unit 100 and the mixer unit 200 several times, the amount of mixed fluid decreases but the mixing is performed. The purity of the fluid can be improved.
  • the outlet side of the mixer unit 200 and the inlet side of the reaction unit 100 are connected. That is, the second discharge pipe 290 corresponding to the outlet side of the mixer unit 200 is connected to the second bypass pipe 301 corresponding to the inlet side of the reaction unit 100.
  • the second bypass pipe 301 is connected to the supply unit 310 via the tank 330.
  • the tank 330 is a storage space for accommodating the mixed fluid and the first fluid, and serves as a buffer. In addition, the tank 330 becomes a space for providing a time for the first fluid to be heated by the heater 390.
  • reaction promoting device 3 is a reaction promoting device for a non-homogeneous fluid in a continuous production mode suitable for mass production.
  • a batch reaction promoting device injects a second fluid into a large container containing the first fluid, while rotating the stirring blade inside the container to mix the first fluid and the second fluid, and then discharge the mixed fluid in the container when the reaction is completed. And a batch manner of filling a new first fluid inside the vessel.
  • this arrangement method has a fixed supply and discharge timing of the fluid, so that continuous operation is impossible and intermittent operation, and the reaction speed is much slower than the reaction promoting device of the present invention.
  • the first fluid is continuously supplied to the reaction tube, and the nozzle installed inside the reaction tube continuously supplies the second fluid, and the reaction tube is capable of sufficiently reacting these non-homogeneous fluids. It extends with a sufficient length so that the injection angle of the nozzle, the injection pressure and the size of the nozzle hole cause sufficient turbulent flow inside the reaction tube, and the area of the interface of the second fluid by the nozzle injection can be maximized. It is optimized to ensure fast and consistent reactivity.
  • the mixer unit 200 may have a rotary blade or a fixed blade installed therein to add mechanical stirring, but may be used as a setler without installing the blade or blade.
  • the settler functions as a separating funnel.
  • triglyceride triglyceride
  • methanol, methoxide as a reactant of a large specific gravity glycerol and a small specific gravity methyl ester is obtained.
  • the glycerol and methyl ester are separated from each other by the difference in specific gravity in the stopped state if left still without any stirring action inside the mixer unit 200 that functions as a settler.
  • the methyl ester separated at the top of the mixer unit 200 is discharged as biodiesel, and the glycerol separated at the bottom is discharged separately.
  • the production method for various reaction modes for the reaction promotion apparatus of the non-homogeneous fluid illustrated in FIGS. 2 and 3 is as follows.
  • the pump 380 is driven to supply the first fluid to the supply unit 310.
  • the first fluid is heated by the heater 390 to adjust the temperature of the first fluid that is optimal for increasing the reaction rate.
  • a tank 390 is installed between the pump 380 and the supply part 310 to be used as a temporary storage space and a heating space of the heater 390.
  • the first fluid supplied through the supply unit 310 fills the reaction tube 110.
  • the second fluid is injected into the fine particles through the nozzle 120 installed inside the reaction tube 110.
  • the desired reaction rate by the interfacial expansion effect by the fine particles, the effect of the fine particles to suppress the generation of fatty acid metal salts on the foam, the chemical effect by the first fluid heating, the physical mixing effect by the turbulent flow inside the reaction tube 110 The transesterification reaction takes place inside the reaction tube (110).
  • the mixed fluid inside the reaction tube 110 is discharged to the outside via the first discharge pipe 190 and the first valve 195.
  • the first valve 195 is in an open state
  • the second valve 295 connecting the reaction unit 100 and the mixer unit 200 is in a closed state.
  • the pump 380 is driven to supply the first fluid into the tank 330, and the first fluid is heated by the heater 390.
  • the second fluid When the first fluid is filled in the reaction tube 110, the second fluid is injected through the nozzle 120.
  • the mixed fluid having the first transesterification reaction is supplied to the mixer unit 200 via the first discharge pipe 190 and the first bypass pipe 201.
  • the first valve 195 since the first valve 195 is in a closed state, the mixed fluid cannot be discharged to the outside.
  • the mixed fluid flows inside the in-line mixer 210 due to the continuity of the fluid, and the transesterification reaction is secondarily performed by the physical mixing force caused by friction and collision with the static blade 212.
  • the mixed fluid passing through the in-line mixer 210 is discharged to the outside via the second discharge pipe 290 and the second valve 295.
  • the third valve 395 located between the mixer unit 200 and the tank 330 is in a closed state.
  • the operation of the pump 380, the heating of the heater 390, the spraying of the nozzle 120, and the operation of the inline mixer 210 are the same as described above.
  • the mixed fluid that has passed through the inline mixer 210 is resupplied to the tank 330 and the reaction unit 100 through the second discharge pipe 290 and the second bypass pipe 301.
  • the transesterification reaction proceeds repeatedly while repeatedly cycling the reaction unit 100 and the mixer unit 200.
  • the driving of the pump 380 is stopped and the mixed fluid contained in the tank 330 is discharged to the outside.
  • the first valve 195 and the second valve 295 are in a closed state, and the third valve 395 connecting the second discharge pipe 290 and the second bypass pipe 301 is in an open state.
  • FIG. 4 to 6 are photographs taken inside the reaction unit 100.
  • FIG. 4 shows before the injection
  • FIG. 5 immediately after the injection
  • FIG. 6 shows the maximum injection state.
  • reaction unit 110 reaction tube
  • fixing plate 112 fixing rod
  • first bypass pipe 210 inline mixer
  • supply part 320 second fluid supply part
  • FIG. 2 shows one embodiment of the reaction promotion apparatus of the non-homogeneous fluid of the present invention which improves the reaction rate and the reaction yield by expanding the surface area of the interface by fine particle spraying.
  • FIG. 3 shows an embodiment in which the embodiment of FIG. 2 is optimized for mass production.
  • FIG. 4 to 6 are photographs taken inside the reaction tube.
  • FIG. 4 shows before injection
  • FIG. 5 immediately after injection
  • FIG. 6 shows a maximum injection state.

Abstract

La présente invention porte sur un appareil d'accélération de réaction en phase hétérogène et sur un procédé l'utilisant pour produire un fluide mélangé, l'appareil comprenant : un tube de réaction contenant un premier fluide pour produire un fluide mélangé à l'aide d'une réaction de transestérification du premier fluide et d'un second fluide ; et une unité de pulvérisation comprenant une buse pour la pulvérisation du second fluide dans le tube de réaction sous la forme de fines particules pour accroître l'interface du second fluide. Selon la présente invention, par pulvérisation du second fluide dans le premier fluide dans le tube de réaction au moyen de la buse, un produit réactionnel mélangé d'une substance hydrophobe et d'une substance hydrophile peut être produit hautement efficacement sur une courte durée. Ici, une réaction de transestérification est effectuée à une vitesse de réaction optimale souhaitée à l'aide d'au moins l'un des effets suivants : un effet d'accroissement d'interface dû à une augmentation de la surface spécifique des fines particules ; un effet consistant en ce que les fines particules empêchent l'apparition de sels métalliques d'acides gras à l'intérieur du tube de réaction ; un effet chimique provoqué par le chauffage du premier fluide ; ou un effet de mélange physique provoqué par un écoulement turbulent à l'intérieur du tube de réaction ou par une unité mélangeur.
PCT/KR2011/005757 2011-08-08 2011-08-08 Appareil et procédé d'accélération de réaction en phase hétérogène pour un fluide WO2013022126A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
KR1020147006169A KR101580583B1 (ko) 2011-08-08 2011-08-08 비동종상 유체의 반응 촉진 장치 및 반응 촉진 방법
PCT/KR2011/005757 WO2013022126A1 (fr) 2011-08-08 2011-08-08 Appareil et procédé d'accélération de réaction en phase hétérogène pour un fluide

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Application Number Priority Date Filing Date Title
PCT/KR2011/005757 WO2013022126A1 (fr) 2011-08-08 2011-08-08 Appareil et procédé d'accélération de réaction en phase hétérogène pour un fluide

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WO2013022126A1 true WO2013022126A1 (fr) 2013-02-14

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CN111097360B (zh) * 2018-10-25 2021-10-01 中国石油化工股份有限公司 具有微孔喷嘴结构的非均相反应器

Citations (4)

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Publication number Priority date Publication date Assignee Title
EP0502638A2 (fr) * 1991-03-04 1992-09-09 Ciba Corning Diagnostics Corp. Analyseur automatisé
US5977251A (en) * 1996-04-01 1999-11-02 The Dow Chemical Company Non-adiabatic olefin solution polymerization
US6159442A (en) * 1997-08-05 2000-12-12 Mfic Corporation Use of multiple stream high pressure mixer/reactor
US20020068836A1 (en) * 2000-05-22 2002-06-06 Monsanto Company Reaction systems for making N- (phosphonomethyl) glycine compounds

Family Cites Families (2)

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Publication number Priority date Publication date Assignee Title
KR20110011092A (ko) * 2009-07-27 2011-02-08 정민아 유화 혼합장치
JP2011178977A (ja) * 2010-03-01 2011-09-15 Kanso:Kk エマルジョン燃料製造装置及びエマルジョン燃料の製造方法

Patent Citations (4)

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Publication number Priority date Publication date Assignee Title
EP0502638A2 (fr) * 1991-03-04 1992-09-09 Ciba Corning Diagnostics Corp. Analyseur automatisé
US5977251A (en) * 1996-04-01 1999-11-02 The Dow Chemical Company Non-adiabatic olefin solution polymerization
US6159442A (en) * 1997-08-05 2000-12-12 Mfic Corporation Use of multiple stream high pressure mixer/reactor
US20020068836A1 (en) * 2000-05-22 2002-06-06 Monsanto Company Reaction systems for making N- (phosphonomethyl) glycine compounds

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KR20140088856A (ko) 2014-07-11

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