WO2001091897A1 - Process and unit for the continuous preparation of isocyanate-containing polyurethane prepolymers - Google Patents
Process and unit for the continuous preparation of isocyanate-containing polyurethane prepolymers Download PDFInfo
- Publication number
- WO2001091897A1 WO2001091897A1 PCT/EP2001/004089 EP0104089W WO0191897A1 WO 2001091897 A1 WO2001091897 A1 WO 2001091897A1 EP 0104089 W EP0104089 W EP 0104089W WO 0191897 A1 WO0191897 A1 WO 0191897A1
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- WIPO (PCT)
- Prior art keywords
- reactor
- process according
- reactants
- isocyanate
- mixture
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/08—Processes
- C08G18/10—Prepolymer processes involving reaction of isocyanates or isothiocyanates with compounds having active hydrogen in a first reaction step
-
- 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
- B01J19/185—Stationary reactors having moving elements inside of the pulsating type
-
- 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
- B01J19/28—Moving reactors, e.g. rotary drums
- B01J19/285—Shaking or vibrating reactors; reactions under the influence of low-frequency vibrations or pulsations
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/08—Processes
- C08G18/0895—Manufacture of polymers by 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
- B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
-
- 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
- B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/00777—Baffles attached to the reactor wall horizontal
Definitions
- This invention relates to a process for the continuous preparation of moderate to high viscosity reaction products requiring moderate to long reaction times (e.g. a polymer(s) including prepolymer(s)).
- moderate to high viscosity reaction products requiring moderate to long reaction times (e.g. a polymer(s) including prepolymer(s)).
- This invention specifically relates to a process and a unit for the continuous preparation of an isocyanate-containing polyurethane prepolymer(s) useful in the production of polyurethane articles.
- the conventional method of making an isocyanate-containing polyurethane prepolymer(s) is to react a polyol and a polyisocyanate batchwise at an elevated temperature.
- Such a process may be a continuous process.
- a continuous process for the preparation of an isocyanate-terminated prepolymer comprising the steps of reacting at least one diisocyanate with one or more substantially linear polyol, according to a molar ratio of 1.3:1.0 to 15.1:1.0.
- the reaction is carried out in a tubular reactor having a ratio length to diameter of at least 2, which is substantially a continuously stirred tank reactor, and with a partial recirculation of the so-obtained products back to the fresh monomer feeds, with which said so-obtained products are intensively mixed.
- the recirculation loop can be achieved in the reactor itself, by using appropriate stirrer, operated at an appropriate rotation speed.
- EP-A-0087817 is disclosed a process for preparing a polyurethane polymer(s) comprising combining an isocyanate and a polyol in a jacketed conduit.
- the jacket contains a heat transfer medium maintained at constant temperature and serves to control the peak of maximum reaction temperature.
- the conduit contains mixing means to produce a plug-shaped velocity profile.
- the means can be a spiral shaped reactor.
- a general object of this invention is therefore to provide a continuous process which enables the preparation of medium to high viscosity compound(s) or polymer(s) requiring a moderate to a long reaction time.
- a further object of this invention is to provide a unit for the continuous preparation of a compound(s) or polymer(s), which is compact, simple to realize and maintain, environmental friendly and could be incorporated into a modular design.
- a specific object of this invention is therefore to provide a continuous process, which enables the preparation of a high quality prepolymer(s).
- Another object of this invention is to provide a unit for the continuous preparation of a prepolymer(s), which are similar to those from a traditional batch production plant, which can operate at medium to high viscosity with moderate to long reaction times sufficient to achieve the conversion desired.
- a further object of this invention is to provide a unit for the continuous preparation of such prepolymer(s), which is compact, simple to realize, operate and maintain, and readily transportable.
- Yet a further object of the invention is to provide a unit for the continuous preparation of a prepolymer(s) which is environmentally friendly.
- the invention resides in a process, preferably adiabatic, carried out in a plug-flow like reactor, with a buffer vessel connected with it. According to an alternate embodiment, the invention resides in a process, preferably adiabatic, carried out in a pulsed perforated plate reactor operated under pulsed conditions.
- a process for the continuous preparation of a chemical compound(s) or polymer(s) comprising the steps of : a) introducing the reactants into a plug flow like reactor which is a perforated plate reactor; b) causing the reactants to react in said reactor under the required pressure and temperature; c) removing the reaction products from said reactor.
- a process for the continuous preparation of an isocyanate-containing polyurethane prepolymer(s), comprising the steps of : (a) introducing reactants into a plug-flow like reactor (l ⁇ )said reactants being at least one isocyanate reactive compound and at least one isocyanate;
- the preferred plug-flow like reactor is a perforated plate reactor for the process above most preferred processes are adiabatic processes.
- the invention provides a continuous process, preferably adiabatic for the preparation of an isocyanate-containing polyurethane prepolymer(s), comprising the steps of:
- the invention also provides a continuous process, preferably adiabatic for the preparation of an isocyanate-containing polyurethane prepolymer(s), comprising the steps of:
- the plug-flow like reactor is a perforated plate reactor.
- the perforated plate reactor is e.g. an elongated vertical vessel
- the heated mixture is introduced at the bottom of said elongated vertical vessel and the reaction product is removed at the top of said elongated vertical vessel, preferably as an overflow.
- the plug-flow like reactor could be any type of plug reactor including a baffled reactor.
- the term "plug-flow like reactor” thus covers the reactor having a residence time distribution substantially close to the plug reactor (e.g. a monodisperse distribution of residence times of 25% around the median value, preferably 20%).
- adiabatic means that there is no heat that is voluntarily exchanged with the reactor; there is no heating or cooling of the reactor during the reaction. This however does not prevent heating the solids into liquids prior to the reaction zone. This also does not prevent heating the reaction mixture at the beginning of the reaction in order to set the starting reaction temperature. In other words, this term “adiabatic” means that there is no attempt to proceed according to an isothermal reaction.
- the perforated plate reactor comprises a series of perforated plates regularly located inside the reactor.
- the fractional free area of each of the perforated plates of the reactor is in the range from 5 to 70, preferably 15 to 35, and most preferably is about 25%.
- the reaction is carried out under pulsed conditions.
- the pulses imposed on the heated reactants mixture have a frequency of 0.1 to 10, preferably 0.5 to 2 Hz.
- the pulses imposed on the heated reactants mixture have superficial amplitude over the sectional cross area of the body of the reactor of 0.5 to 50, preferably 1 to 15 mm, most preferably 2 to 10 mm.
- the pulses are imposed on said heated reaction mixture while it is introduced into said perforated plate reactor.
- the pulses are typically imposed on said heated reaction mixture by moving the perforated plates of said reactor and or the liquid.
- the heated mixture is obtained by mixing the first reactant with the second reactant and then heating the mixture.
- the inlet temperature can be achieved by heating or cooling either in line or off line such as in the feed storage tank.
- the heated mixture is obtained by mixing the first reactant with the preheated second reactant.
- the heated mixture is obtained by mixing the first reactant with the preheated second reactant and then heating the obtained mixture.
- the heated mixture is obtained by mixing the first preheated reactant with the preheated second reactant and then heating the obtained mixture.
- the process further comprises a step of cooling the reaction product.
- the process further comprises a step of filtering the (cooled) reaction product.
- the heated mixture entering the reactor typically has a viscosity in the range from 0.15 cP to 2000 cP, preferably from 2 cP to
- cP 10,000 cP, preferably from 0.8 cP to 2000 cP, especially from 0.8 cP to 400 cP (cP is mPa.s).
- the process further comprises a step of recirculating the obtained product to the feed inlet zone.
- the invention also resides in a unit for the continuous preparation of products of a polymer(s) comprising (a) inlet means for the reactant(s);
- the invention finally also resides in a unit for the continuous preparation, preferably adiabatic of a compound(s) or a polymer(s) comprising:
- pulse generating means (11) for imposing pulses on the content of the perforated plate reactor (10).
- the invention also resides in a unit for the continuous preparation of an isocyanate- containing polyurethane prepolymer(s), comprising: (a) inlet means for at least one isocyanate reactive compound and at least one isocyanate;
- the invention finally also resides in a unit for the continuous preparation, preferably adiabatic, of an isocyanate-containing polyurethane prepolymer(s), comprising: (a) inlet means for at least one isocyanate reactive compound and at least one isocyanate (l,2,2a,5);
- pulse generating means (11) for imposing pulses on the content of the perforated plate reactor (10).
- the plug-flow like reactor is a perforated plate reactor.
- the unit further comprises heating or cooling means for heating or cooling the reaction product either within the reactor or after exiting from the buffer vessel.
- the unit also comprises filtering means, located after the reactor, notably after said cooling means, for filtering the (cooled) reaction product.
- the unit further comprises shutdown recirculation means for (full) recirculating the (cooled) reaction product through the heating, mixing (and pulse) generating means, the (perforated plate) reactor, optionally the buffer and optionally the cooling means, at the end of the production run.
- Figure 1 is a block flow sheet for the process of the invention
- Figure 2 is a schematic vertical cross-section along B-B of the perforated plate reactor of the unit of the invention.
- Figure 3 is a schematic horizontal cross-section along A-A of the perforated plate reactor of the unit of the invention.
- the process and the unit of the invention are particularly suitable for mildly exothermic, neutral or very mildly endothermic addition reactions, which have moderately high viscosity reactants and reaction products.
- mildly exothermic is herein intended to designate those reactions which generate heat up to a point where the temperature is below the temperature at which some products would begin degrading (e.g. hazing, yellowing, etc.).
- temperature increase can be up to 50°C (or even more), while generally it is up to 20°C.
- mildly endothermic is herein intended to designate those reactions which consume heat to an extent that does not prevent these reactions.
- the temperature drop is usually up to 20°C, preferably up to 10°C.
- moderate high viscosity is herein intended, in general, from 20 to 2000 cP (mPa.s).
- an organic polyisocyanate is used.
- a first reactant which is an organic polyisocyanate composition is introduced through line 1, pump 2 and line 3 to a feeds mixer 4 where it is mixed with an isocyanate reactive compound introduced through line 5, pump 2a and preheated by preheater 6.
- the feeds mixer can be, e.g., a simple mixing valve or a dynamic mixer or a static mixer, the latter one being preferred.
- the pumps operating the system are preferably of the diaphragm type. This allows to handle compositions that may contain some small solids, such as MDI at low temperature; this is an advantage over classical gear pumps.
- the diaphragm pumps are thus robust. They are also suited for transportation.
- the pumps are also preferably of the ganged type, i.e. one drive shaft (one motor) powers several pumps.
- the pumps are also preferably connected directly to the feed. This avoids to have recourse to the classical burdensome circulation loop.
- the conduits, especially of the isocyanate side, are preferably heated, e.g. by an electrical tracing on the feed lines.
- the heaters used in the instant unit can be of any classical type. Preferably they are of the finned type, i.e. a cylindrical heater in a conduit has lateral fins on its central element.
- the mixer is placed preferably immediately after the feed streams meet, e.g. just before the heater. It can also be before the entry of the reactor (especially when no heating is foreseen before the reactor).
- This mixer can be of any type. Preferably, it is a static mixer, of the type with a packing in it.
- the organic polyisocyanate composition may be selected from the group consisting of aliphatic, cycloaliphatic and araliphatic polyisocyanates, especially diisocyanates, like hexamethylene diisocyanate, isophorone diisocyanate, cyclohexane-l,4-diisocyanate, 4,4'- dicyclohexylmethane diisocyanate and m- and p- tetramethylxylylene diisocyanate, and in particular aromatic polyisocyanates like tolylene diisocyanates (TDI), phenylene diisocyanates and most preferably methylene diphenyl isocyanates having an isocyanate functionality of at least two.
- diisocyanates like hexamethylene diisocyanate, isophorone diisocyanate, cyclohexane-l,4-diisocyanate, 4,4'- dicyclohexylmethane diisocyan
- Methylene diphenyl isocyanates are preferred.
- the methylene diphenyl isocyanates (MDI) may be selected from pure 4,4' -MDI, isomeric mixtures of 4,4'-MDI and 2,4'-MDI and less than 10 % by weight of 2,2'-MDI, crude and polymeric MDI having isocyanate functionalities above 2, and modified variants thereof containing carbodiimide, uretonimine, isocyanurate, urethane, aliphanate, urea or biuret groups.
- methylene diphenyl isocyanates are pure 4,4' -MDI, isomeric mixtures with 2,4' -MDI optionally containing up to 50 % by weight of polymeric MDI and uretonimine and/or carbodiimide modified MDI. Mixtures of methylene diphenyl isocyanates with in particular up to 25 % by weight to other polyisocyanates mentioned above may be used if desired.
- the isocyanate reactive compound is one that comprises a hydrogen atom that is able to react with the isocyanate, e.g. hydroxy or amine hydrogen.
- the isocyanate reactive compound is preferably a polyol, which may be selected from the group consisting of polyether polyols, polyester polyols, polyestera ides polyols, polythioether polyols, polycarbonate polyols, polyacetal polyols, polyolefin polyols, and the like.
- a preferred polyol is a polyether polyol, especially those comprised of propylene oxide PO and/or ethylene oxide EO (tipped or random).
- Additives, if needed, are preferably introduced through line 7 and pump 8 into feeds mixer 4.
- the mixture exiting from feeds mixer 4 is then heated in reactants heater 9 to a temperature in the range from 45 to more than 200°C and preferably from 60 to 130°C.
- the heated mixture flows to the plug-flow like reactor 10 via unit 11 (pulsation unit) where it reacts.
- a typical NCO content is e.g. from 2 to 31%, preferably from 5 to 25%, by weight.
- the residence time is comprised between 5 min and 5 h, preferably between 10 and 90 min, most preferably between 15 and 45 min.
- the time reduction is a great advantage over classical batch reactors.
- the following is a side-by-side comparison (values given for the invention are exemplary only).
- the time is expressed in minutes.
- the gain over the prior art is thus of more than 8 hours.
- the plug-flow like reactor is exemplified here as a perforated plate reactor 10.
- the following description is given with respect to a perforated plate reactor.
- the reactor is fitted with a pulse unit 11 which gives an oscillating motion to the reaction mixture in addition its steady upwards motion.
- This pulse unit may comprise e.g. a pump of the diaphragm type (but without the non-return valves).
- the pulses imposed on the heated reactants mixture have a frequency from 0.1 to 10 and preferably from 0.5 to 2 Hz.
- the amplitude of the pulses is in the range from 0.5 to 50, preferably 1 to 15 mm, more preferably 2 to 10 mm. Amplitudes are given peak-to-peak.
- the reaction product exiting from the top of perforated plate reactor 10 flows then to a buffer vessel 12.
- the function of the buffer vessel 12 is to provide a high flexibility to the unit of the invention. Firstly, it ensures a smoother product outlet flow. Secondly, it enables the reactor 10 to overflow, rather than be hard piped into the outlet system; hence, the reactor can be an atmospheric rather than a pressure vessel. (By atmospheric is also meant the presence of a nitrogen blanket over the reactor; the associated pressure is however negligible). This reduces the weight, the cost and the complexity of the unit, since there could be no need to fit with a complex overpressure protection system. Thirdly, the buffer vessel acts as a buffer when there is a process upset downstream of the unit, which gives the operator time to solve the problem before the unit has to shut down. This reduces product quality risks from such upsets.
- the buffer vessel can be avoided (while it is preferably present especially under atmospheric conditions).
- a process run under a pressure higher than atmospheric pressure may also be run without the buffer vessel, even when there is no pulse conditions (although the pulse regime is preferred).
- the product exiting from buffer vessel 12 is cooled by product cooler 13 (such as a spiral heat exchanger) and filtered by product filter 14.
- a shutdown recirculation line 15 is provided between product cooler 13 and product filter 14. It links the exit of product cooler 13 to the inlet of feeds mixer 4. This feature minimizes the waste due to production of so-called "off-spec" material (i.e. material that is outside the desired ranges of parameters) at the end of the production run, since the content of the plant is recirculated through the equipment until the reaction is finished.
- Such a recirculation also enables the plant to be cooled down before emptying the plant, reducing the risk that remaining prepolymer builds up in the equipment, which would increase maintenance or cross-contamination risks.
- the buffer vessel 12 When recirculating the plant at the end of a production run, the buffer vessel 12 acts as a reservoir. As fluid contracts when cooled, this buffer capacity of fluid aids in recirculating and cooling the fluid.
- the perforated plate reactor 10 is an elongated vertical vessel, which is in the form of a cylindrical column. It contains a series of stationary perforated plates disposed in a substantially parallel way and at substantially regular intervals along the longitudinal axis X of the column.
- a perforated plate 16 is most visible on Figure 3. It comprises several substantially identical and circular perforations 17, which are regularly located in the plate 16. The number and diameter of the perforations 17 are such that the fractional free area of the plate, i.e. the sum of the areas of all perforations 17, is in general at least 5, especially in the range from 10 to 50, preferably 15 to 35, and most preferably is about 25%.
- the space between two successive plates is from 10 to 500 mm, preferably from 50 to 200 mm, most preferably from 100 to 150 mm.
- the dimensions of the reactor can be the following: inner diameter is from 50 to 2000 mm, preferably from 100 to 500 mm; height is from 0.5 to 10 m, preferably from 2 to 6 m. The number of plates can thus be determined by dividing the height by the spacing of the plates.
- the diameter of the holes in the perforated plates may vary; it is e.g. from 4 to 12 mm, preferably from 6 to 10 mm.
- the perforated plates 16 need not be fixed to the internal wall of reactor 10.
- the plates can also be fixed to an inner axle which is itself fixed to the reactor.
- the perforated plates can be mounted on a shaft inside the reactor 10, and the shaft is given an oscillating motion by the pulse unit 11.
- the content of the reactor 10 also has, besides its steady upward motion, an effectively oscillating motion caused by the motion of the plates 16.
- the perforated plates 16 are replaced by plates with slots, expanded metal, other baffle arrangements with free areas arranged sufficiently close together to generate cross-mixing or jet when a pulse is imposed.
- the plates are generally perpendicular to the axis of the reactor; inclined plates are also envisaged, e.g. to improve the free-draining properties.
- the plug-flow like reactor 10 (preferably a perforated plate reactor), especially in adjunction with the pulse unit 11, brings several advantages : it enables longer reaction times with a narrow residence time distribution, hence approaching batch behavior for elements of reaction mixture passing through the reactor.
- the flow of the reaction mixture nearly achieves a plug-flow behavior.
- this is achieved with no rotating parts in contact with the process fluid, which simplifies design, improves reliability and reduces the weight and maintenance costs of the reactor.
- the reactor also drains out well and therefore minimizes waste between products.
- the pulse unit moderates the start-up temperatures, since the mass of the pulse- generating unit on the inlet to the reactor acts as a heat sink and helps achieve accurate temperature control at start-up. This also minimizes the production of "off-spec" material.
- Another advantage provided by the use of the plug-flow like reactor is that it enables the reaction to be carried out in conditions closed to adiabatic conditions, which simplifies the design of the unit, no accurate temperature control of the reactor being necessary, which in turn allows to vary the diameter of the reactor.
- a further unique feature of the unit of the invention is that it can be constructed as a packaged plant. The unit can then be transported in standard transport containers and it is robust for transportation to any location where the manufacturing is to take place.
- the robust compact pumping, the preheating, the plug-flow like reactor operated under atmospheric pressure, the perforated plate reactor, the buffer vessel, the static mixer, fast reaction time and other items depicted above, are embodiments which can be used alone or in combination on a given unit (such as a traditional unit, e.g. a batch unit).
- the unit requires only standard site services found at many warehouse sites, i.e. electricity, optionally cooling water, compressed air (a nitrogen bottled supply is appropriate).
- the reaction product can be fed to a drum filling system, road tankers or bulk storage tanks.
- the invention thus provides a mobile plant unit that can be operated virtually anywhere in the world.
- the unit is thus unique in its ability to be easily transportable while providing high quality products, over a wide range of viscosities.
- the unit of the invention is preferably a mobile unit. It has been hitherto designed as a stand-alone unit, but it can also interface into a more complex manufacturing chain.
- the invention can also be applied to other reactions characterized by moderately viscous fluids with moderate long reaction times. Especially those reactions where high conversion are required i.e. polymerisation reactions and / or biological reactions, are preferred.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Polyurethanes Or Polyureas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Other Resins Obtained By Reactions Not Involving Carbon-To-Carbon Unsaturated Bonds (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP01940315A EP1292389A1 (en) | 2000-05-31 | 2001-04-10 | Process and unit for the continuous preparation of isocyanate-containing polyurethane prepolymers |
AU2001273936A AU2001273936A1 (en) | 2000-05-31 | 2001-04-10 | Process and unit for the continuous preparation of isocyanate-containing polyurethane prepolymers |
JP2001587902A JP2003535166A (en) | 2000-05-31 | 2001-04-10 | Method and apparatus for continuous preparation of isocyanate-containing polyurethane prepolymers |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB0013068A GB0013068D0 (en) | 2000-05-31 | 2000-05-31 | Process and unit for continuous preparation of isocyanate-containing polyurethane prepolymers |
GB0013068.2 | 2000-05-31 | ||
GB0013066A GB0013066D0 (en) | 2000-05-31 | 2000-05-31 | Process and unit for continuous preparation of isocyanate-containing polyurethane prepolymers |
GB0013066.6 | 2000-05-31 |
Publications (1)
Publication Number | Publication Date |
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WO2001091897A1 true WO2001091897A1 (en) | 2001-12-06 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/EP2001/004089 WO2001091897A1 (en) | 2000-05-31 | 2001-04-10 | Process and unit for the continuous preparation of isocyanate-containing polyurethane prepolymers |
Country Status (5)
Country | Link |
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EP (1) | EP1292389A1 (en) |
JP (1) | JP2003535166A (en) |
CN (1) | CN1444504A (en) |
AU (1) | AU2001273936A1 (en) |
WO (1) | WO2001091897A1 (en) |
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WO2005120695A1 (en) * | 2004-06-14 | 2005-12-22 | Tema Technopolymers S.R.L. | Plant for manufacturing polyurethane goods |
WO2006136850A1 (en) * | 2005-06-23 | 2006-12-28 | Nitech Solutions Limited | Method and apparatus for fluid-liquid reactions |
US7435787B2 (en) | 2005-09-14 | 2008-10-14 | Momentive Performance Materials Inc. | Process for the continuous production of silylated resin |
CN101970398A (en) * | 2008-03-14 | 2011-02-09 | Dic株式会社 | Process for producing urethane (meth)acrylate |
WO2012007419A1 (en) * | 2010-07-13 | 2012-01-19 | Bayer Materialscience Ag | Process for preparing polyurethane prepolymers containing isocyanate groups |
EP3160932B1 (en) | 2014-06-24 | 2018-03-14 | Covestro Deutschland AG | Process for producing nitrobenzene |
WO2020201171A1 (en) | 2019-04-01 | 2020-10-08 | Basf Se | Continuous production of polyurethane prepolymers |
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EP2311554A1 (en) * | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Method for reaction control of exothermic reaction and apparatus therefore |
JP2017516905A (en) * | 2014-06-06 | 2017-06-22 | コベストロ、ドイチュラント、アクチエンゲゼルシャフトCovestro Deutschland Ag | Method for continuous production of stable prepolymers |
KR102362979B1 (en) * | 2019-12-26 | 2022-02-16 | 주식회사 삼양사 | Isocyanate prepolymer product with improved storage stability and method for preparing the same |
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EP0087817A1 (en) * | 1982-03-03 | 1983-09-07 | Castle & Cooke Techniculture, Inc. | Continuous polymer process apparatus and system |
JPS60244280A (en) * | 1984-05-18 | 1985-12-04 | Mitsubishi Heavy Ind Ltd | Aeration and agitation tank |
DE4327805A1 (en) * | 1992-08-18 | 1994-02-24 | Du Pont | Polyurethane prepolymer prodn. and appts. used - by microwave heating a liq. mixt. of poly:diol and di:isocyanate and stirring in an annular reactor |
US5316821A (en) * | 1991-03-08 | 1994-05-31 | Nkk Corporation | Partition plate for multiple-stage adsorption separator |
US5750080A (en) * | 1994-09-09 | 1998-05-12 | Urea Casale S.A. | Method for in-situ modernization of a urea synthesis reactor |
-
2001
- 2001-04-10 AU AU2001273936A patent/AU2001273936A1/en not_active Abandoned
- 2001-04-10 EP EP01940315A patent/EP1292389A1/en not_active Withdrawn
- 2001-04-10 JP JP2001587902A patent/JP2003535166A/en not_active Withdrawn
- 2001-04-10 CN CN 01813376 patent/CN1444504A/en active Pending
- 2001-04-10 WO PCT/EP2001/004089 patent/WO2001091897A1/en not_active Application Discontinuation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
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EP0087817A1 (en) * | 1982-03-03 | 1983-09-07 | Castle & Cooke Techniculture, Inc. | Continuous polymer process apparatus and system |
JPS60244280A (en) * | 1984-05-18 | 1985-12-04 | Mitsubishi Heavy Ind Ltd | Aeration and agitation tank |
US5316821A (en) * | 1991-03-08 | 1994-05-31 | Nkk Corporation | Partition plate for multiple-stage adsorption separator |
DE4327805A1 (en) * | 1992-08-18 | 1994-02-24 | Du Pont | Polyurethane prepolymer prodn. and appts. used - by microwave heating a liq. mixt. of poly:diol and di:isocyanate and stirring in an annular reactor |
US5750080A (en) * | 1994-09-09 | 1998-05-12 | Urea Casale S.A. | Method for in-situ modernization of a urea synthesis reactor |
Non-Patent Citations (1)
Title |
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PATENT ABSTRACTS OF JAPAN vol. 010, no. 120 (C - 343) 6 May 1986 (1986-05-06) * |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2005120695A1 (en) * | 2004-06-14 | 2005-12-22 | Tema Technopolymers S.R.L. | Plant for manufacturing polyurethane goods |
EP1609525A1 (en) * | 2004-06-14 | 2005-12-28 | Tema Technopolymers S.r.l. | Plant for manufacturing polyurethane goods. |
WO2006136850A1 (en) * | 2005-06-23 | 2006-12-28 | Nitech Solutions Limited | Method and apparatus for fluid-liquid reactions |
US7435787B2 (en) | 2005-09-14 | 2008-10-14 | Momentive Performance Materials Inc. | Process for the continuous production of silylated resin |
CN101970398A (en) * | 2008-03-14 | 2011-02-09 | Dic株式会社 | Process for producing urethane (meth)acrylate |
WO2012007419A1 (en) * | 2010-07-13 | 2012-01-19 | Bayer Materialscience Ag | Process for preparing polyurethane prepolymers containing isocyanate groups |
CN103025779A (en) * | 2010-07-13 | 2013-04-03 | 拜耳知识产权有限责任公司 | Process for preparing polyurethane prepolymers containing isocyanate groups |
US8835591B2 (en) | 2010-07-13 | 2014-09-16 | Bayer Intellectual Property Gmbh | Method for preparing polyurethane prepolymers containing isocyanate groups |
CN103025779B (en) * | 2010-07-13 | 2015-10-14 | 拜耳知识产权有限责任公司 | The method of the polyurethane prepolymer of preparation containing isocyanate group |
EP3160932B1 (en) | 2014-06-24 | 2018-03-14 | Covestro Deutschland AG | Process for producing nitrobenzene |
US11136285B2 (en) | 2014-06-24 | 2021-10-05 | Covestro Deutschland Ag | Process for producing nitrobenzene |
WO2020201171A1 (en) | 2019-04-01 | 2020-10-08 | Basf Se | Continuous production of polyurethane prepolymers |
Also Published As
Publication number | Publication date |
---|---|
AU2001273936A1 (en) | 2001-12-11 |
EP1292389A1 (en) | 2003-03-19 |
JP2003535166A (en) | 2003-11-25 |
CN1444504A (en) | 2003-09-24 |
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