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US20030133857A1 - Multiphase polymerization reactor - Google Patents

Multiphase polymerization reactor Download PDF

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Publication number
US20030133857A1
US20030133857A1 US10/044,714 US4471402A US2003133857A1 US 20030133857 A1 US20030133857 A1 US 20030133857A1 US 4471402 A US4471402 A US 4471402A US 2003133857 A1 US2003133857 A1 US 2003133857A1
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US
United States
Prior art keywords
reactor
heat transfer
heat
heat pipe
reaction
Prior art date
Legal status (The legal status 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 status listed.)
Abandoned
Application number
US10/044,714
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English (en)
Inventor
Vinh Le
Syed Ahmed
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Saudi Basic Industries Corp
Original Assignee
Saudi Basic Industries Corp
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
Application filed by Saudi Basic Industries Corp filed Critical Saudi Basic Industries Corp
Priority to US10/044,714 priority Critical patent/US20030133857A1/en
Assigned to SAUDI BASIC INDUSTRIES CORPORATION reassignment SAUDI BASIC INDUSTRIES CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AHMED, SYED, LEE, VINH N.
Priority to US10/501,387 priority patent/US20060182668A1/en
Priority to PCT/US2002/041770 priority patent/WO2003059958A2/fr
Priority to EP02806528A priority patent/EP1470378A4/fr
Priority to AU2002367034A priority patent/AU2002367034A1/en
Priority to KR1020030001663A priority patent/KR100997570B1/ko
Publication of US20030133857A1 publication Critical patent/US20030133857A1/en
Abandoned legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
    • F28D1/06—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with the heat-exchange conduits forming part of, or being attached to, the tank containing the body of fluid
    • 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
    • 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
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/04—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/00033—Continuous processes
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00121—Controlling the temperature by direct heating or cooling
    • B01J2219/0013—Controlling the temperature by direct heating or cooling by condensation of reactants

Definitions

  • the present invention relates to an improved chemical reaction apparatus which is capable of removing large heat fluxes from a reaction mixture while maintaining the reaction mixture at essentially isothermal conditions.
  • the invention also relates to a method of conducting chemical reactions, and in particular, multi-phase polymerization reactions, at essentially isothermal conditions using the novel reactor of the invention.
  • a batch type reactor capable of handling high heat flux without internal cooling coils, reflux cooling and/or the circulation of the reaction mixture through an external cooler would be highly desirable with respect to many isothermal chemical reactions and in particular with respect to multi-phase polymerization reactions.
  • the chemical reactor of the present invention comprises a conventional tank reactor equipped with a heat transfer device commonly referred to as a heat pipe.
  • heat pipes utilize evaporation of a cooling fluid from a porous medium affixed to a heat transfer surface to absorb heat.
  • a heat pipe system is applied to the external surface of a tank reactor opposite the reaction mixture in the reactor to remove the heat of reaction from the reaction mixture by evaporative cooling through the heat transfer surface of the heat pipe.
  • the porous medium on the heat transfer surface is commonly referred to as a “wick”.
  • the evaporation of the cooling fluid from the porous medium enjoys extremely good heat transfer coefficients and enables extremely high heat flux at essentially isothermal conditions.
  • the evaporated heat transfer fluid is then condensed and returned to the heat transfer zone of the reactor. Since heat transfer coefficients associated with condensation are also high, both the heat absorption and heat release segments of the heat pipe equipped reactor enjoy very high heat flux rates.
  • a heat pipe heat transfer system is applied to the external surface of a tank reactor.
  • a reactor so equipped can be operated in either batch or continuous mode.
  • the reactor of the invention can be a stirred tank reactor when desirable.
  • the heat release segment of heat pipe equipped tank reactor relies upon the condensation of the heat transfer fluid which can take place in a condenser which is remote from the reactor, so that the surface area available for cooling need not be limited to the area of the tank reactor's external surface. Accordingly, condenser(s) with sufficient surface area to handle the required heat flux can be located away from the tank reactor of the invention while still being in close proximity to it.
  • a tank reactor equipped with a heat pipe heat exchange device according to the present invention can be operated at essentially isothermal conditions. Because the heat transfer coefficients for evaporation are significantly higher than those for convection, especially when the heat transfer surface is porous as in the case of a heat pipe, the reactor of the present invention enjoys substantially greater heat flux than would be possible with conventional jacket cooling of a tank reactor.
  • the heat pipe cooled tank reactors of the present invention are suitable for emulsions, suspensions and viscous polymer syrups because they do not have internal or external circulating loops, which can cause emulsions and suspensions to lose stability and which can be fouled with viscous polymer incrustations.
  • Polymerization reactions conducted in multiple phase systems are particularly advantaged in the reactor of the present invention.
  • These polymer systems can be solutions of polymer or co-polymers and their respective monomers suspended in water (emulsion and suspension polymerization), solutions of polymers and their monomers in water suspended in oils (inverse emulsion and suspension polymerization) and many other possibilities.
  • Examples of monomers or co-monomers which can be advantageously polymerized to their corresponding polymers in the reactor of the invention are:
  • the process surface is not subject to fouling because the reactor temperature is uniform since the evaporation and condensation of the heat transfer fluid occurs at the same uniform temperature, and cold and hot spots in the reactor are avoided.
  • the choice of the material of construction, the choice of the internal working fluid and the design of the wick structure for the heat pipe apparatus of the invention is within the capability of those skilled in the art.
  • the materials of construction in contact with the heat transfer fluid are commonly selected from copper and copper alloys, aluminum and its alloys and stainless steel and other ferrous metal alloys.
  • heat “pipe” and “tank” reactor are used in the description of this invention, innumerable configurations are possible, some of which are far from the cylindrical shape of a conventional pipe or tank.
  • possible shapes could be, but not limited to, flat, rectangular, annular, polygonal or tubular.
  • the isothermal chemical reactors of the present invention can utilize either sealed or thermosyphon heat pipe heat transfer devices.
  • the sealed heat pipe is comprised of three sections: (1) an evaporator section where heat is absorbed by vaporizing a liquid heat transfer medium, (2) an adiabatic section where the vaporized heat transfer medium flows without changing state, and (3) the condenser section where the vaporized heat transfer medium is condensed using an external source of cooling.
  • the heat transfer medium condensate returns to the evaporator section by the wicking action of the porous surface or wick in the evaporator section.
  • wicking is a surface tension phenomenon that may be limited in long heat pipes by liquid head, if a particular reaction would require a reactor in which the reaction mixture would occupy a reaction zone having a large vertical dimension, it is sometimes preferred to operate the reactor of the invention with the heat pipe heat transfer device in a horizontal position.
  • a large vertical reaction zone can be divided into multiple heat pipe heat transfer zones each having height and a corresponding wick height which can be wetted by capillary action of the heat transfer fluid in the wick.
  • thermosyphon heat pipe embodiment of the invention can utilize gravity or pumps to return condensed heat transfer fluid to the evaporator section through piping which is distinct from that used to convey vaporized heat transfer fluid from the evaporator section of heat pipe to the condenser.
  • a source of liquid heat transfer fluid which advantageously can be clean boiler feed water can feed the evaporator section of the reactor heat pipe and the evaporator section can communicate with a vapor header, such as a steam header.
  • a vapor header such as a steam header.
  • reaction temperature is regulated by the boiling point of the heat transfer fluid.
  • pressure of the heat transfer fluid it is possible to vary the boiling point of the heat transfer fluid. In many cases the temperature over the entire reactor can be controlled to within 1 degree centigrade.
  • the heat pipe reactor of the present invention adds intermediary steps to the overall heat transfer mechanism, the heat transfer flux of the reactor surface can be enhanced by several orders of magnitude over conventional convection cooling.
  • the fast rate of heat transfer with fluid evaporation on a porous surface and the rapid transport of the vapors from the evaporator section to the condenser section of the heat pipe contribute to this superior performance.
  • the heat transfer fluid is chosen to assure trouble free heat pipe operation depending on the temperature of operation. It can be selected from liquids having the desired boiling point at a selected operating pressure. Common heat transfer fluids are water, acetone, alkanes, ammonia, fluorocarbons and aromatic solvents.
  • the wick utilized in the invention can be comprised of fiber mats, sintered metal powders of single size or multiple sizes of spherical or non-spherical shape, and metal screens in single or multiple layers.
  • FIG. 1 illustrates a perspective view of a reactor according to the invention having multiple sealed heat pipe heat transfer devices of the pipe jacket type.
  • FIG. 2 illustrates a perspective view of a reactor according to the invention having multiple thermosyphon heat pipe heat transfer devices of the pipe jacket type with individual condensers.
  • reactor 10 constructed according to the present invention is illustrated.
  • reactor 10 is equipped with feed nozzle 11 , outlet 12 and stirring device 20 .
  • reaction mixture 30 comprised of reactants and reaction products, the relative concentrations of which will vary as the selected reaction proceeds.
  • Reaction mixture 30 fills reactor 10 to level L.
  • Reactor 10 is equipped with annular jacket type heat pipe units 40 a - d.
  • Heat pipe units 40 a - d respectively each have wicked reactor wall heat transfer surfaces 41 a - d; annular spaces 42 a - d, and condenser heat transfer surfaces 43 a - d.
  • Heat transfer fluid 44 is in annular spaces 42 a - d.
  • Heat transfer fluid 44 is in the liquid phase at the bottom of annular spaces 42 a - d and is the vapor phase in the balance of annular spaces 42 a - d.
  • Cooling liquid jacket 50 surrounds heat pipe heat transfer units 40 a - d. Cooling liquid W is fed into cooling liquid jacket 50 at cooling jacket inlet 51 and flows from jacket 50 at cooling jacket outlet 52 .
  • reactor 10 is filled with reaction mixture 30 comprised of the chemical compounds to be reacted.
  • reaction mixture 30 can include one or more catalysts.
  • Reactor 10 is stirred using stirring device 20 .
  • Reaction mixture 30 is at a temperature selected to encourage the reaction of the reactants to one or more desirable products. Because the reaction of the reactants to the desired product is isothermic, means must be provided to remove the heat of reaction.
  • the heat of reaction from reaction mixture 30 flows through the walls of reactor 10 to wicked reactor wall heat transfer surfaces 41 a - d. Wicked reactor wall heat transfer surfaces 41 a - d are wetted with heat transfer fluid 44 from a pool of fluid 44 at the bottom of annular spaces 42 a - d.
  • the heat transfer fluid 44 has a boiling point which is essentially the same as the desired reaction temperature for reaction mixture 30 .
  • the height of heat pipe heat transfer units 40 a - d is selected so that the capillary action of wicked reactor wall heat transfer surfaces 41 a - d is sufficient to overcome the liquid head created by the wetting of wicked reactor wall heat transfer surfaces 41 a - d.
  • the heat of reaction from reaction mixture 30 causes heat transfer fluid 44 to vaporize in wicked reactor wall heat transfer surfaces 41 a - d and thereby absorb the heat of reaction. Vaporized heat transfer fluid 44 flows through annular spaces 42 a - d until it comes in contact with condenser heat transfer surfaces 43 a - d.
  • Vaporized heat transfer fluid 44 condenses on condenser heat transfer surfaces 43 a - d and releases the heat of reaction to condenser heat transfer surfaces 43 a - d, through which the heat of reaction flows to cooling liquid W in cooling liquid jacket 50 .
  • Cooling liquid W which may be cooling water, is sent to cooling liquid recovery where its temperature is reduced to a predetermined temperature for cooling liquid feed.
  • FIG. 2 a preferred embodiment of the reactor of the invention having multiple thermosyphon heat pipe heat transfer devices with individual condensers is illustrated.
  • Components in FIG. 2 which operationally correspond to components in FIG. 1, either bear the same number as FIG. 1 or the same number plus 100.
  • reactor 110 differs from the reactor depicted in FIG. 1 by the substitution of thermosyphon heat pipe units 140 a - d for the sealed heat pipe heat units 40 of FIG. 1.
  • Thermosyphon heat pipe units 140 a - d respectively have wicked reactor wall heat transfer surfaces 141 a - d, and annular spaces 142 a - d.
  • Thermosyphon heat pipe units 140 a - d have vapor outlet lines 62 a - d at their upper ends which communicate with, respectively, condensers 60 a - d.
  • Vaporized heat transfer fluid 44 flows through annular spaces 142 a - d and vapor outlet lines 62 a - d to condensers 60 a - d. Heat transfer fluid 44 is in the liquid phase at the bottom of annular spaces 142 a - d and is conveyed by capillary action into wicked reactor wall heat transfer surfaces 141 a - d.
  • the heat of reaction from reaction mixture 30 flows through the walls of reactor 110 to wicked reactor wall heat transfer surfaces 140 a - d .
  • the heat of reaction causes heat transfer fluid 44 to vaporize and flow through vapor outlet lines 62 a - d to condensers 60 a - d, wherein evaporated heat transfer fluid 44 is condensed in conventional fashion using cooling water or other heat transfer means.
  • Condensed heat transfer fluid 44 is returned by gravity or pumping through heat pipe feed lines 61 a - d to thermosyphon heat pipe units 140 a - d.
  • Acrylamide is soluble in water but not in organic liquids such as C5-C14 alkanes.
  • Polyacrylamide forms a gel in water. This polymer gel is suspended in alkane for ease of handling. It is undesirable to cool the acrylamide/polyacrylamide reactant/product mixture by circulating the process fluid through an external heat exchanger because of the possibility of fouling the heat exchanger with the polymer gel.
  • Direct reflux cooling through the evaporation of water (which is more volatile than the alkane) is not considered because (a) the low temperature would require the reactor to operate under vacuum and (b) the returned reflux (water) would create a third phase in the reactor. Therefore the necessity of handling high heat release usually limits the acrylamide/polymerization to relatively small batches. Since the surface to volume ratio of a reactor increases with decreasing batch size, small reactors have higher heat flux capacity per unit volume than larger reactors.
  • a 60 m 3 batch reactor is used to produce a polyacrylamide, the reactor dimensions are 12 ft ID by 18 ft long.
  • Such a batch reaction mixture consists of 20,000 kg of water, 20,000 kg of acrylamide and 20,000 kg of hexane.
  • the reaction temperature is 25 ° C. and the batch time is 3 hours.
  • the density of all components is assumed to be 1000 kg/m 3 .
  • the heat of reaction is 2,140 kW. It is also assumed that chilled water at 15° C. is available to remove the heat of reaction.
  • heat pipe jackets 40 a - d would preferably be made of copper.
  • Conventional water jacket 50 surrounds heat pipe jackets 40 a - d .
  • the maximum heat removal capacity of this embodiment of the invention is approximately 900 kW which is 73% greater than the conventionally cooled reactor. Nevertheless, the heat removal capacity of this embodiment of the invention is also less than is required for reactor of the size proposed.
  • thermosyphon heat pipe jackets 140 with individual condensers 60 can also be applied to the instant reaction. However, because of liquid head limitations in heat transfer units 140 , seven such units are required on the shell of the reaction and one for the bottom head of the reactor.
  • the average heat flux in the thermosyphon heat pipe units is approximately 29 kW/m 2 . Since the total heat transfer average of the thermosyphon heat pipe units 140 is approximately 75 m 2 , the reactor of FIG. 2 has sufficient heat transfer capacity to handle the heat of reaction for the 60 m 3 batch reactor. Since the heat transfer area of condensers 70 is not limited to the available reactor jacket surface, a total of approximately 180 m 2 of condenser surface can be provided to handle the necessary heat flux.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Combustion & Propulsion (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Polymerisation Methods In General (AREA)
  • Other Resins Obtained By Reactions Not Involving Carbon-To-Carbon Unsaturated Bonds (AREA)
US10/044,714 2002-01-12 2002-01-12 Multiphase polymerization reactor Abandoned US20030133857A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
US10/044,714 US20030133857A1 (en) 2002-01-12 2002-01-12 Multiphase polymerization reactor
US10/501,387 US20060182668A1 (en) 2002-01-12 2002-12-31 Multiphase polymerization reactor
PCT/US2002/041770 WO2003059958A2 (fr) 2002-01-12 2002-12-31 Reacteur de polymerisation multiphase
EP02806528A EP1470378A4 (fr) 2002-01-12 2002-12-31 Reacteur de polymerisation multiphase
AU2002367034A AU2002367034A1 (en) 2002-01-12 2002-12-31 Multiphase polymerization reactor
KR1020030001663A KR100997570B1 (ko) 2002-01-12 2003-01-10 다중 중합 반응기

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US10/044,714 US20030133857A1 (en) 2002-01-12 2002-01-12 Multiphase polymerization reactor

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US10/501,387 Continuation US20060182668A1 (en) 2002-01-12 2002-12-31 Multiphase polymerization reactor

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US20030133857A1 true US20030133857A1 (en) 2003-07-17

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US10/501,387 Abandoned US20060182668A1 (en) 2002-01-12 2002-12-31 Multiphase polymerization reactor

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US (2) US20030133857A1 (fr)
EP (1) EP1470378A4 (fr)
KR (1) KR100997570B1 (fr)
AU (1) AU2002367034A1 (fr)
WO (1) WO2003059958A2 (fr)

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EP1617705A2 (fr) 2005-10-05 2006-01-18 Phonak AG Prothèse auditive avec adaptation in-situ
CN105983382A (zh) * 2015-02-13 2016-10-05 江苏康鹏农化有限公司 一种生产农药用反应釜
CN109569483A (zh) * 2019-01-02 2019-04-05 安徽瑞邦生物科技有限公司 一种新型高效水解釜
WO2019117989A1 (fr) * 2017-12-15 2019-06-20 Google Llc Structure tridimensionnelle à refroidissement à changement de phase intégré
CN110404497A (zh) * 2019-07-31 2019-11-05 北京六合宁远科技有限公司 一种多取代溴氟取代苯丙咪唑化合物的制备方法
CN112316865A (zh) * 2021-01-05 2021-02-05 蓬莱禄昊化工机械有限公司 一种不锈钢反应釜外盘管加热套
CN113230998A (zh) * 2021-05-11 2021-08-10 崔魁 一种日用化学品反应釜及使用方法

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KR101645472B1 (ko) * 2014-10-28 2016-08-04 손창민 다기능 화학 장치
CN105352339B (zh) * 2015-08-11 2019-04-23 中国矿业大学 一种用于化工的蒸发冷凝器
PL3440119T3 (pl) 2016-04-08 2022-01-24 Ineos Europe Ag Jednostka polimeryzacyjna i sposób polimeryzacji
CN111111575A (zh) * 2019-12-27 2020-05-08 北京英惠尔生物技术有限公司 一种提高Vc酯反应釜效率的方法及其简易冷水供给系统

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CN109569483A (zh) * 2019-01-02 2019-04-05 安徽瑞邦生物科技有限公司 一种新型高效水解釜
CN110404497A (zh) * 2019-07-31 2019-11-05 北京六合宁远科技有限公司 一种多取代溴氟取代苯丙咪唑化合物的制备方法
CN112316865A (zh) * 2021-01-05 2021-02-05 蓬莱禄昊化工机械有限公司 一种不锈钢反应釜外盘管加热套
CN113230998A (zh) * 2021-05-11 2021-08-10 崔魁 一种日用化学品反应釜及使用方法

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WO2003059958A2 (fr) 2003-07-24
WO2003059958A3 (fr) 2003-11-20
AU2002367034A1 (en) 2003-07-30
EP1470378A4 (fr) 2006-02-01
KR20030062251A (ko) 2003-07-23
US20060182668A1 (en) 2006-08-17
AU2002367034A8 (en) 2003-07-30
EP1470378A2 (fr) 2004-10-27

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