• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Circular reactor for continuously carrying out and controlling reactions in liquid and / or gaseous media, wherein the reactor has at least one pipeline (2) with a pipe start (3) and a pipe end (4) and at least one static mixer arranged in the pipeline (2). Heat exchanger (1) with a in the pipe (2) arranged heat exchanger and in the pipeline (2) arranged static mixing elements comprises. The heat exchanger has a heat exchanger surface A 1 and a void volume V 1, which is defined by the length of the heat exchanger along the pipe (2) and the cross section of the pipe section over this length. The pipeline (2) has at least one point between the pipe start (3) and the pipe end (4) on a return with a pump (5). The ratio (A 1 / V 1) between the heat exchanger surface A 1 and the void volume V 1 is at least twice as large as the ratio (A 2 / V 2) of a pipe vane of identical construction with void volume V 2 with static mixing elements and one void volume V 2 enveloping heat exchanger, which defines the heat exchanger surface A 2.
    公开号:CH705823B1
    申请号:CH02533/12
    申请日:2012-11-26
    公开日:2016-08-31
    发明作者:Georg Alain；Andreoli Silvano；Vögeli Tobias；Altenburger Daniel；Eiholzer Adrian
    申请人:Fluitec Invest Ag；
    IPC主号:
    专利说明:

    Technical area
    The invention relates to a circulation reactor according to the preamble of claim 1 for the continuous implementation and control of reactions in liquid and / or gaseous media with a mixer, with a heat exchanger and with a pump, wherein the circulation reactor at least one pipe with a Beginning of the tube and a pipe end and arranged at least one arranged in the pipeline mixer, wherein the heat exchanger has a void flowing through the media and a void adjacent to the heat exchanger surface, wherein the pipe at least one point between the pipe start and the pipe end a return with a pump having.
    State of the art
    A chemical reactor is that part of a plant in which chemical processes take place and in which chemical reactions are carried out. Such reactors are operated in batch processes in which, for example, a certain amount of a product is produced per production cycle or in a continuous mode of operation.
    Switching a batch process to continuous operation provides several key benefits, such as increased security, consistent product quality and maximum economy. However, the continuous mode of production requires the consideration of various factors such as kinetics, thermodynamics, selectivity and energy flows already in the planning phase. If sufficient account is taken of these key quantities, a continuous reaction can be achieved safely, consistently and with the greatest possible space / time yields. Once put into operation, continuous processes offer several key benefits such as:- improved reaction control- small reaction volume- no dead zones- stable operation- no cleaning and loading times- small space requirement etc.
    With appropriately designed experiments in the reaction calorimeter, stirred reactor or even in a simple beaker, a wealth of technical information on the relationships can be obtained such as: reaction rate (kinetics), heat of reaction and chemical equilibrium (thermodynamics), selectivity, conversion, by-products, viscosity curve , required energy dissipation to the mixture, temperature dependence of the reaction rate according to Arrhenius, etc.
    The data from the batch reactor can be transferred to continuously operating tubular reactors. Taking into account the mixing efficiency and the heat flows, the reaction time in the batch reactor becomes the residence time in the continuous tubular reactor. In the continuous tube reactor, the time of the greatest heat generation can be predicted with local precision. Volume, residence time, specific surface area and heat dissipation can only be realized to a large extent without restrictions by means of cascades or circulation reactors.
    At very high heat of reaction cycle reactors must be used, which have a complete backmixing and by the recirculation causes a dilution effect. This can have a negative effect on the selectivity and thereby achieved space / time exploitation. For this reason, cycle reactors are also followed by additional residence time lines with minimal back-mixing.
    For years, continuous cycle reactors have been used, for example, for the following reactions: polymer preparation, esterifications, nitrations, diazotizations, rearrangements, alkylations, halogenations, hydrogenations, oxidations, polymerizations, neutralizations, etc.
    The term circulation reactor used here is derived from the reaction technology, where loop reactors resp. Circular reactors are widely used to monitor exothermic reactions.
    Such cycle reactors typically include a single-circulation pump, dynamic or static mixers and / or additional heat exchangers such as plate or shell and tube heat exchangers for heat removal. High heat transfer combined with the highest possible mixing efficiency can reduce the circulation rate in the continuous tubular reactor, which immediately affects the reaction, energy consumption and production costs. Typical ratios of circulation rate to total inflow rate are in the range of 15 to 100, which is in many cases too high in scale-up and leads to significant operating and pumping costs. The feed streams consist for example of educts such as monomers, catalysts, solvents, initiators, regulators, additives and / or stoppers. These additives are also referred to below as reactants.
    Next, tube-like housing are known from the prior art, which are equipped with at least one mixing insert arranged therein, for example in the form of one or more webs and slots having plate (s). In each case, the webs of a plate extend through the slots of the other plate crossing therethrough. Preferably, the plates are inclined relative to each other and to the axis of the tube. For temperature control (cooling and / or heating), for example, the tubular housing is equipped with a double jacket, wherein the heat exchanger thus surrounds the pipe jacket. As a result, these reactors are also referred to as identically constructed reactors.
    The said identical reactors or geometrically similar static mixer heat exchangers are generally characterized by the fact that the ratio of heat exchange surfaces to void volume, also referred to as A / V ratio, decreases with increasing tube diameter. In the case of a scale-up, therefore, the heat exchange performance decreases dramatically. Therefore, static mixers with sheath are only suitable for small throughputs, or massively increases the recirculation flow, which usually has a negative impact on the energy balance and the end product. Another possibility is the parallelization of the currents, which leads to an increased metering and control engineering effort.
    If the equipped with the mixing elements flow tube is additionally equipped with an internally arranged tube bundle, the ratio of heat exchange surface to the empty tube volume, also referred to as A / V ratio, despite constant pipe diameter constant or at least kept very large. The internally arranged tube bundle consists of additional small heat exchange tubes, which are flowed through inside with heat transfer fluid for heat exchange. However, internally located tube bundles dramatically degrade mixing performance.
    Thus, for example, the heat exchanger according to DE 2,839,563 a very low mixing performance, especially since the tube bundles are able to mix only in one axial direction. It must therefore be switched several bundles rotated by 90 ° in series to achieve a mixing performance at all. For such apparatus, the term static mixer heat exchanger is basically wrong. More suitable static mixer heat exchangers are, for example, those of the CSE-XR type. In these mixer heat exchangers, the mixing performance is adjustable by the arrangement of the sheets. A static mixer-heat exchanger of this kind is known from EP 1 067 352 B1 and WO 2008/141 472.
    For the comparison of the mixing power, one generally uses the relative standard deviation S / S0 or the coefficient of variation COV. With these known mixed quality materials, it should be noted that only measurement results can be recorded with the same measurement analyzes. In the literature, measurements are taken by means of conductivity measurement, decolorization, laser-induced fluorescence (LIF) or by means of photometric analysis FIP (Fluitec Image Processing). Only measurements with the same methods may be compared, otherwise significant deviations will occur. If a laminar flow static mixer heat exchanger achieves a relative standard deviation S / S0 of 0.05 by means of photometric analysis at a L / D ratio of at least 20, then a well mixing static mixer heat exchanger can be used. Preferably, static mixer heat exchangers achieve a relative standard deviation S / S0 of 0.05 at an L / D ratio of at least 12.
    Presentation of the invention
    The invention has for its object to provide an improved continuously operating and provided with a heat exchanger circulation reactor, in particular comprising a tubular reactor, which eliminates the above-mentioned disadvantages of the prior art. In particular, the tubular reactor should have an improved performance with respect to the mixing behavior and the heat exchange during the reaction.
    Such a problem is solved by the subject matter of claim 1, in that the mixer used is a static mixer with integrated heat exchanger, in which the mixing elements adjacent to the void volume (V1) and form a substantial portion of the heat exchanger surface (A1).
    Preferably, a circulation reactor for continuous implementation and control of reactions in liquid and / or gaseous media comprises at least one pipe with a pipe start and a pipe end and at least one arranged in the pipeline static mixer heat exchanger with a pipe arranged in the heat exchanger and in the pipeline arranged static mixing elements. The heat exchanger defines a heat exchanger surface and a void volume defined by the length of the heat exchanger along the pipe and the cross-section of the pipe section over that length. The pipeline has at least one point between the beginning of the pipe and the pipe end a return to a pump, which allows the continuous operation. Further, the ratio between the heat exchanger surface and the void volume of said mixer-heat exchanger, at least twice, more preferably at least four times, as large as the ratio of a void volume identical tubular reactor with static mixing elements and a void volume enveloping the heat exchanger, which defines the heat exchanger surface.
    By choosing the appropriate ratio, the tubular reactor has improved heat exchange properties. In addition, the performance of the reactor with respect to the mixing process is also positively influenced. Consequently, the mixing performance can be increased overall. Furthermore, the choice of the corresponding ratio allows a scaling of the system.
    The circulation reactor may consist of a tubular reactor and a material recycling. With a continuous cycle, a reaction can be achieved with the properties between a tubular reactor and an ideally mixed stirred tank reactor.
    Preferably, the entire volume of the circulation reactor is filled with static mixer heat exchangers, so that over the entire tubular reactor, the heat dissipation is ensured.
    Preferably, the void volume defined by the volume of the pipe or the corresponding pipe section minus the volume of the static mixing element, minus the volume of the arranged in the pipe section heat exchanger and, if available, minus the additional volume consisting of the small tubes. The volume of the tube is defined by the length of the tube section over which the heat exchanger and the static mixer extend, and the cross-sectional area of the tube via this section.
    A reactor of identical construction is typically understood to mean a reactor which comprises a static mixer and a heat exchanger which surrounds or surrounds this pipe section in a pipe section. The heat exchanger thus essentially surrounds the pipe section, which according to the above definition determines the void volume accordingly. The heat exchanger can be provided as a tubular housing with a double jacket.
    The mixing insert of the static mixer is preferably provided in the form of one or more webs and slots having plates that reduce the void volume.
    In each case, the webs of a plate extend through the slots of the other plate crossing through. Preferably, the plates are inclined relative to each other and to the axis of the tube.
    Preferably, the void volume enveloping heat exchanger of the same reactor completely envelopes the void volume.
    Preferably, at least one point between the beginning of the pipe and the pipe end an opening into the pipe interior feed for at least one additional feed stream is connected. By means of this feed, further substances can be introduced into the mixing process.
    Preferably, the static mixer heat exchanger at least one cooled section or at least one heated section. Thus, the reaction can thus be cooled or heated.
    Preferably, at least one feed opening into the recirculation is connected to the recirculation with the pump for at least one additional feed stream, which has the advantage that further substances of the reaction can be added via the recirculation.
    The heat exchanger may comprise in an advantageous embodiment, in addition to the heat exchanger elements integrated in the static mixer elements and a jacket heat exchanger surrounding the tube of the reactor.
    Further embodiments are given in the dependent claims.
    Further advantages of the present invention will become apparent from the following: The inventive circulation reactor should be for slow, normal and fast reactions in all flow areas, preferably in the laminar flow area, can be used and ensure a largely immediate and complete mixing. A practical classification of the reaction rate is based on the half-life. This is the time tH after which the starting material has half reacted at a certain temperature, that is, the conversion has reached Ui = 0.5. One calls reactions with:- tH> 1 min as slow- 1 s <tH <1 min as normal- 1 ms <tH <1 s as fastTH <1 ms as very fast.
    The only additional influencing variable is in this case only the mixing efficiency of the reactor used. In particular, in multi-phase reactions (liquid / liquid or gas / liquid) or when using solid or dispersed catalysts intimate mixing is very important, because the mass transfer is limited by the different stationary boundary layers. For such reactive tasks in a circulation reactor, a static mixer is particularly suitable. A static mixer heat exchanger is also suitable for mixing the reactants in a circulation reactor.
    Brief description of the drawings
    Further advantages, features and details of the invention will become apparent from the following description of preferred embodiments and from the drawing, which is merely illustrative and not restrictive interpreted. The drawing shows schematically in<Tb> FIG. 1 <SEP> a circulation reactor with a static mixer heat exchanger; and<Tb> FIG. 2 <SEP> a circulation reactor with three static mixer heat exchangers, the circuit in addition two shut-off valves and two purge valves.
    Description of preferred embodiments
    Fig. 1 shows a circulation reactor for the continuous implementation and control of slow, normal and rapid, exothermic reactions in liquid and / or gaseous media.
    The circulation reactor for the continuous implementation and control of reactions in liquid and / or gaseous media comprises at least one pipe 2 with a pipe start 3 and a pipe end 4 and at least one arranged in the pipeline 2 static mixer heat exchanger 1. The static mixer Heat exchanger comprises a arranged in the pipe 2 heat exchanger and arranged in the pipe 2 static mixing elements. Heat exchangers and mixers are thus arranged inside the tube and thus come into direct contact with the substances to be mixed and tempered. As such a static mixer heat exchanger can be configured by way of example according to EP 1 067 352 or WO 2008/141 472. The heat exchanger serves to exchange heat between the fluid flowing in the pipeline, and the static mixing elements serve to mix the fluid.
    The heat exchanger has a heat exchanger surface A1 and a void volume V1. The heat exchanger surface is defined by the surface used for the heat exchange. The void volume is determined by the length of the heat exchanger along the pipe 2 and the cross section of the pipe section over said length. The void volume corresponds to the volume of the tube minus the volume of the static mixing element used with integrated heat exchanger. The heat exchanger therefore extends over the said length along the pipe section.
    Between the heat exchanger surface A1 and the void volume V1, a ratio A1 / V1 can be formed. The ratio A1 / V1 between the heat exchanger surface A1 and the void volume V1 of the said mixer-heat exchanger is at least twice, more preferably at least four times as large as the ratio A2 / V2 of a tube vessel with static mixing elements that is identical with respect to void volume V2 and a heat exchanger surrounding the void volume V2 Heat exchanger surface A2definiert.
    Under the empty volume V2umumüllenden heat exchanger is essentially understood a jacket heat exchanger, which extends completely around a corresponding pipe section around. Usually, this is a jacket heat exchanger, which extends around it on the outside of the pipe section.
    In other words, it can also be stated that the ratio of the heat exchange surfaces A1 to the void volume V1 of the mixer-heat exchanger at least twice, more preferably at least four times as large as that of a comparable in length and outer tube diameter tubular reactor with static mixing elements.
    As can be seen in Fig. 1, the pipe 2 at at least one point between the pipe start 3 and the pipe end 4 a return with a pump 5. The return opens between the pipe start 3 and mixer-heat exchanger 1 and between Mixer heat exchanger 1 and pipe end 4 in the pipeline 2. Thus, the tubular reactor can be operated continuously in the circuit.
    The circulation reactor may have at least one feed 6 for at least one additional feed stream at any location of the pipeline 2. The return may also have additional feeds. The feed streams consist for example of educts such as monomers, catalysts, solvents, initiators, regulators, additives and / or stoppers. These additives are also referred to below as reactants.
    Fig. 2 shows a circulation reactor for the continuous implementation and control of slow, normal, rapid and exothermic reactions in liquid and / or gaseous media. Identical parts are provided with the same reference numerals and have the same property as described with reference to FIG. 1.
    The reactor of FIG. 2 consists of at least one pipe 2, a return with a pump 5, at least one static mixer-heat exchanger 1 in the return and at least one static mixer-heat exchanger 1 after the return to the pump. 5 These static mixer heat exchangers 1 have the same properties with respect to the ratios described above as the static mixer heat exchanger 1 according to FIG. 1. The return with the pump 5 has at least one inlet immediately after the pump 5 and directly in front of the first static mixer heat exchanger. At this point, the reaction begins, so that the chemically generated, high heat of reaction in the loop can be well controlled.
    The two shut-off valves 7, which are preferably positioned dead space at the beginning and at the end of the return before entering the pipe 2, can be completely or partially closed during continuous operation. This allows the use of a flexible continuous reactor which, in operation, can be switched to a continuous tubular reactor or to a continuous reactor cascade instead of the loop reactor. However, this is only possible if the ratio of the circulation rate to the total feed rate is low, since otherwise the first static mixer heat exchanger 1 can not be used simultaneously for all three reactor circuits. In other words, the recirculation rate can be adjusted by a corresponding control unit with an inlet control and shut-off valve control, wherein temperature parameters, viscosity signals or other parameters for the progress of the chemical reaction and flow rates of the inflow can be used as parameters.
    The valves 8 are used to purge and purify the recycle with the pump 5 when switching to the continuous tubular reactor or to the continuous reactor cascade.
    Examples
    In the following, comparative examples and embodiments according to the invention are presented to illustrate the resulting advantageous A / V ratios.
    A continuous conventional circulation reactor, constructed in principle as the embodiment of FIG. 1, but with static mixers, a total of 5 l h <-> <1> reactants are supplied. The conventional circulation reactor is also referred to herein as a structurally identical reactor. The circulation reactor has static mixer heat exchangers of the type CSE-X from Fluitec Georg AG with an internal diameter of ∅ 27.3 mm. The mixer has a shell heating, so a shell heat exchanger. The circulation reactor has a recirculation of 75 l h <-> <1>, the reaction has a reaction enthalpy of 220 kJ kg <-> <1>. 80% of the reaction is reacted in the circulation reactor. The average residence time is 60 s for 80% conversion, the pressure loss in the loop is about 0.2 bar at a viscosity of 1000 mPas. The ratio of circulation rate to feed rate is in the range of 15. With this reactor construction, the reaction can be monitored isothermally at a heat exchanger temperature of 7 ° C. and a heat exchanger amount of 200 l h -1. The A / V ratio is 209 m <2> m <-> <3>.
    It should now be a scale-up of this example to 500 l h <-1>, which corresponds to a recirculation rate of 7500 l h <-1>. The circulation reactor 2 has static mixer heat exchangers of the type CSE-X from Fluitec Georg AG with an internal diameter of ∅ 68.8 mm. The mixer has a jacket heating. The reaction has a reaction enthalpy of 220 kJ kg <-> <1>. 80% of the reaction is reacted in the circulation reactor 2. The mean residence time is 60 s for 80% conversion, the pressure loss in the loop is about 3.5 bar at a viscosity of 1000 mPas. The ratio of the circulation rate to the feed rate is in the range of 15. With this reactor construction, the reaction can be controlled isothermally at a heat exchanger temperature of -32 ° C. and a heat exchanger quantity of 10 000 l h -1. The A / V ratio is 64 m <2> m <-3>. The ratio has thus deteriorated to less than 1/3 due to the scale-up from 209 m <-> <1>.
    It is now according to another comparative example, a scale-up to 500 lh <-> <1> take place, which corresponds to a recirculation rate of 7500 lh <-> <1> when the circulation reactor to the static mixer heat exchangers of the type CSE-X from Fluitec Georg AG with an inner diameter of ∅ 106.3 mm also has a jacket heating. The reaction has a reaction enthalpy of 220 kJ kg <-> <1>. 80% of the reaction is reacted in the circulation reactor. The average residence time is 60 s for 80% conversion, the pressure loss in the loop is about 0.2 bar at a viscosity of 1000 mPas. The ratio of the circulation rate to the feed rate is in the range of 15. With this reactor construction, the reaction can be monitored isothermally at a heat exchanger temperature of -130 ° C. and a heat exchanger quantity of 10 000 l h <->. The A / V ratio is 41.4 m <2> m <-3>. It is only about one fifth of the unscaled example.
    When scale-up according to an embodiment of the invention to 500 lh <-> <1> with a static mixer heat exchanger of the type CSE-XR Fluitec Georg AG, with an inner diameter of ∅ 106.3 mm, there is actually a Reduction of the recirculation rate to 2500 lh <-1>. Since the mixer heat exchanger has a jacket heating and an internal tube bundle heating, the A / V ratio increases from 41.4 m <2> m <-3> to 227 m <2> m <-> compared to a conventional static mixer heat exchanger. 3>, which gives more than a factor of 5 in said ratio A2 / V2 of a reactor of the same type. In a simpler embodiment can be dispensed with the use of a jacket heating for the tubular reactor.
    The reaction has a reaction enthalpy of 220 kJ kg <-> <1>. 80% of the reaction is reacted in the circulation reactor 3. The mean residence time is 60 s for 80% conversion, the pressure loss in the loop is about 1.0 bar at a viscosity of 1000 mPas. The ratio of the circulation rate to the feed rate is only 5. With this reactor design, the reaction at a heat exchanger temperature of 23 ° C and a heat exchanger amount of 10 000 l h <-1> are controlled isothermally.
    For the pilot scale at 5 l h -1, static mixers perform excellently and prove themselves for numerous applications in chemical reaction engineering. Due to the decreasing A / V ratio, the temperature in the circuit must be drastically reduced during scale-up, for example from 7 ° C to -32 ° C or even to -130 ° C. This means that, for example, no more water can be used for the cooling, but for example methanol or liquid gas, which leads to an increasing apparatus and control engineering effort.
    With reference to FIG. 2, the following may be noted: A circulation reactor for continuously carrying out and controlling slow, normal, rapid and exothermic reactions in liquid and / or gaseous media has a pipeline 2 with at least one recirculation with a pump 5 , in which at least one static mixer heat exchanger 1 is arranged, the ratio of the heat exchange surfaces to the void volume at least twice, more preferably at least four times as large as that of a comparable in length and outer tube diameter tubular reactor with static mixing elements.
    权利要求:
    Claims (11)
    [1]
    1. circulation reactor for continuously carrying out and controlling reactions in liquid and / or gaseous media with at least one mixer (1), with a heat exchanger and with a pump (5),wherein the circulation reactor comprises at least one pipe (2) with a pipe start (3) and a pipe end (4) and the at least one mixer (1) arranged in the pipe (2),the heat exchanger having a void volume V1 traversed by the media and a heat exchanger surface A1 adjacent to the void volume,wherein the pipeline (2) has at least one point between the pipe start (3) and the pipe end (4) a return to the pump (5),characterized in that the mixer (1) is a static mixer with mixing elements, wherein the heat exchanger is integrated in the static mixer and together they form a static mixer heat exchanger, wherein the mixing elements adjoin the void volume V1 and form a substantial portion of the heat exchanger surface A1.
    [2]
    2. Circulation reactor according to claim 1, characterized in that the static mixer with the integrated heat exchanger (1) has the shape of a tubular reactor in which the ratio A1 / V1 between the heat exchanger surface A1and the void volume V1 of said mixer-heat exchanger is at least twice as large the ratio A2 / V2 of a tube reactor with static mixing elements, which is identical with respect to empty volume V2, and a heat exchanger enveloping the void volume V2, which defines the heat exchanger surface A2.
    [3]
    3. Circulation reactor according to claim 1, characterized in that said ratio A1 / V1 is at least four times as large as said ratio A2 / V2 of the reactor of the same type.
    [4]
    4. Circulation reactor according to one of the preceding claims, characterized in that the void volume enveloping the heat exchanger completely envelopes the void volume.
    [5]
    5. Circulation reactor according to one of the preceding claims, characterized in that the reactions are slow, normal, rapid and / or exothermic reactions, reactions with a half-life tH> 1 min slowly, reactions with 1s <tH <1 min normal and reactions with 1 ms <tH <1 s are to be described as fast and wherein the half-life tH is the time after which a reactant is half reacted at a certain temperature.
    [6]
    6. Circulation reactor according to one of the preceding claims, characterized in that at least one point between the pipe start (3) and the pipe end (4) opening into the pipe interior feeder (6) is connected for at least one additional feed stream.
    [7]
    7. Circulation reactor according to one of claims 1 to 5, characterized in that connected to the return to the pump (5) at least one opening into the return feed (6) for at least one additional feed stream.
    [8]
    8. Circulation reactor according to one of the preceding claims, characterized in that the static mixer-heat exchanger (1) has at least one cooled section, or the static mixer-heat exchanger (1) has at least one heated section.
    [9]
    9. circulation reactor according to one of the preceding claims, characterized in that the return to the pump (5) shut-off valves (7), with which the recirculation rate on the return is adjustable.
    [10]
    10. Circulation reactor according to one of the preceding claims, characterized in that the return to the pump (5) has at least one purge valve (8).
    [11]
    11. Circulation reactor according to one of the preceding claims, characterized in that the heat exchanger in addition to the heat exchanger elements integrated in the static mixer elements also comprises a jacket heat exchanger surrounding the tube of the reactor.
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    同族专利:
    公开号 | 公开日
    CH705823A2|2013-05-31|
    EP2596860A1|2013-05-29|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE2839563A1|1978-09-12|1980-03-27|Hoechst Ag|METHOD FOR CONTINUOUS MASS POLYMERIZATION OF ALKENYL FLAVORS|
    DE19618678A1|1996-05-09|1997-11-13|Basf Ag|Process for the production of polystyrene by continuous anionic polymerization|
    DE19638094A1|1996-09-18|1998-03-19|Basf Ag|Process for the preparation of methyl methacrylate polymers in a circulation reactor|
    EP1067352B1|1999-07-07|2003-08-27|Fluitec Georg AG|Heat exchange device|
    DE602007006754D1|2006-01-13|2010-07-08|Akzo Nobel Coatings Int Bv|CIRCUIT REACTOR FOR POLYMERIZATION AND METHOD FOR THE CLEANING THEREOF|
    TWI461237B|2006-08-08|2014-11-21|Sulzer Chemtech Ag|An apparatus for the combined carrying out of heat exchange and static mixing using a liquid|
    AT498810T|2007-05-24|2011-03-15|Atlas Holding Ag|FLOW CHANNEL FOR A MIXER HEAT EXCHANGER|EP2881154B1|2013-12-04|2018-02-21|Fluitec Invest AG|Method and device for flash evaporation|
    SG11201803824RA|2015-11-11|2018-06-28|Fluitec Invest Ag|Device for carrying out a chemical reaction in a continuous method|
    EP3181221A1|2015-12-16|2017-06-21|Fluitec Invest AG|Method for monitoring a chemical reaction and a reactor|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    EP11190732.5A|EP2596860A1|2011-11-25|2011-11-25|Loop-type reactor fitted with a heat exchanger|
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