WO2015022079A1 - Procédé et dispositif de transformation de polymères/produits de polymérisation en solution en éléments moulés en polymère - Google Patents

Procédé et dispositif de transformation de polymères/produits de polymérisation en solution en éléments moulés en polymère Download PDF

Info

Publication number
WO2015022079A1
WO2015022079A1 PCT/EP2014/002240 EP2014002240W WO2015022079A1 WO 2015022079 A1 WO2015022079 A1 WO 2015022079A1 EP 2014002240 W EP2014002240 W EP 2014002240W WO 2015022079 A1 WO2015022079 A1 WO 2015022079A1
Authority
WO
WIPO (PCT)
Prior art keywords
polymer
fluid
degassing
preconcentration
pump
Prior art date
Application number
PCT/EP2014/002240
Other languages
German (de)
English (en)
Inventor
Andreas Diener
Daniel Witte
Original Assignee
List Holding Ag
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 List Holding Ag filed Critical List Holding Ag
Publication of WO2015022079A1 publication Critical patent/WO2015022079A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
    • B29B7/58—Component parts, details or accessories; Auxiliary operations
    • B29B7/72—Measuring, controlling or regulating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
    • B01D1/222—In rotating vessels; vessels with movable parts
    • B01D1/223—In rotating vessels; vessels with movable parts containing a rotor
    • B01D1/225—In rotating vessels; vessels with movable parts containing a rotor with blades or scrapers
    • B01D1/226—In rotating vessels; vessels with movable parts containing a rotor with blades or scrapers in the form of a screw or with helical blade members
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0005—Degasification of liquids with one or more auxiliary substances
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0021—Degasification of liquids by bringing the liquid in a thin layer
    • B01D19/0026—Degasification of liquids by bringing the liquid in a thin layer in rotating vessels or in vessels containing movable parts
    • 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
    • B01J19/1862—Stationary reactors having moving elements inside placed in series
    • 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
    • B01J19/20—Stationary reactors having moving elements inside in the form of helices, e.g. screw reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
    • B29B7/7461—Combinations of dissimilar mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
    • B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
    • B29B7/7485—Systems, i.e. flow charts or diagrams; Plants with consecutive mixers, e.g. with premixing some of the components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/84—Venting or degassing ; Removing liquids, e.g. by evaporating components
    • B29B7/845—Venting, degassing or removing evaporated components in devices with rotary stirrers
    • B29B7/847—Removing of gaseous components before or after mixing
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments
    • C08F6/001—Removal of residual monomers by physical means
    • C08F6/003—Removal of residual monomers by physical means from polymer solutions, suspensions, dispersions or emulsions without recovery of the polymer therefrom
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments
    • C08F6/008—Treatment of solid polymer wetted by water or organic solvents, e.g. coagulum, filter cakes
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments
    • C08F6/06—Treatment of polymer solutions
    • C08F6/10—Removal of volatile materials, e.g. solvents
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments
    • C08F6/06—Treatment of polymer solutions
    • C08F6/12—Separation of polymers from solutions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B9/00—Making granules
    • B29B9/02—Making granules by dividing preformed material
    • B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
    • B29B9/065—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion under-water, e.g. underwater pelletizers

Definitions

  • the invention relates to a process for the conversion of polymers / solution polymers into polymer molded articles, wherein the polymer is subjected to a treatment in a preconcentration and / or a main evaporation and / or a degassing and a shaping.
  • CONFIRMATION COPY Essentially degasify main evaporation stage and then finally treated in a finisher to a desired concentration of volatiles.
  • the object of the invention is the development of a complete and efficient technology, from the assumption of the polymer / solution polymer from the polymerization also with very low polymer contents, existing components of the conventional technology with new components must be linked together so that the polymers / polymers from the newly developed polymer chemistry processes can be processed and transferred with appropriate product quality in polymer moldings.
  • the polymer / polymer is fed before treatment to a washing stage.
  • the existing process for the direct evaporation of polymers precedes a washing stage and adds further options within the process steps in order to obtain an overall technology for the solution of the problem.
  • the additionally added washing step a washing process of the polymer / polymer, is necessary to remove non-volatile, but soluble components from the polymer / polymer, wherein the polymer / polymer is mixed with water or another liquid and separated again by the difference in density.
  • the preconcentrated, heated and pressurized polymer solution is transported via a distributed metering (see DE 10 2009 007 641.7) in the main evaporator and from there into the degasser. Both processes can be operated under vacuum, normal pressure and overpressure. The required product quality is set in the degasser. However, the discharge of the degasser provides a very compact mass, which can not be used by the processing industry. It has therefore been necessary to incorporate a granulation followed by polymer molding production which makes it possible to produce a polymer mold which will allow the existing polymer processing processes to continue.
  • a three-way valve is installed after the degasser so that off-spec material remains inside the ExZone.
  • the polymer molding can optionally be a comminution with downstream transport in the air stream or a so-called underwater granulation followed by transport in the water.
  • the pneumatic transport air can be actively moistened, so that the particles do not stick to each other or to the wall of the pneumatic transport line, whereby the water additionally cools due to evaporation.
  • Fluid bed cooler and a baler connected.
  • the fluid bed cooler has been converted to a fluidized bed temperer because the polymer from the degasser needs no further drying, but must have optimum temperature conditions for subsequent molding.
  • the baler gives the polymer the desired shape.
  • the bales are checked for foreign parts and weight, packed and stored.
  • In the case of use of the granulation in water (underwater granulation) are cooled, the polymer granules in the water carried in the water stream, then separated from the water, dried, and also compressed into bales or big bag filled 's.
  • Polymers in the context of the present invention are, for example, but not limited to, thermoplastics, thermoplastic elastomers, rubbers or other polymers.
  • a process according to the invention for the workup of solution polymers into polymer molded articles comprises the following steps: a) a preconcentration of a first fluid (B) comprising at least one nonvolatile polymer and at least one volatile compound having a polymer content of 2% by weight to 35% by weight.
  • the preconcentration takes place by single or multi-stage successive heating of the fluid (B) under pressure and subsequent expansion into a flash vessel, whereby vapors are removed via the vapor line and the flash vessel works with or without recycling of the preconcentrated fluid (C), wherein the recycle of the preconcentrated fluid (C) is mixed with the fresh fluid (B) before heating or separately heated again in a flash vessel to a concentrated fluid (C) having a polymer content of 20 wt .-% to 85 wt. -% to obtain.
  • a molding comprising a tempering and a packaging, wherein the discharged fluid (E) by a construction that is grown directly at the outlet of the pressure increasing the degassing system, comminuted and tempered into small particles and wherein the tempered polymer granules transported pneumatically and a shaping be supplied.
  • the temperature of fluid (B) at the inlet of the preconcentration is in the range of 10 to 100 ° C.
  • the viscosity of fluid (B) at the inlet of the preconcentration is in the range from 100 mPa.s to 500,000 mPa.s.
  • the fluid (B) is brought to a temperature of 60 ° to 350 ° C in the pre-concentration step.
  • the flash evaporation is operated at a pressure of 100 mbar to 10 bar.
  • a multi-stage flash evaporation is driven with decreasing pressure.
  • the flash container is a vertical container which can be equipped with or without stirrer.
  • the bottom of the vertical container is either a horizontal, stirred vessel with heatable elements, or a conically shaped and heated bottom, in which the discharge by means of pressure-increasing unit, which in turn may comprise a pump or a screw design or a combination of both , transported to the main evaporation stage.
  • the viscosity of fluid (C) is in the range of 500 Pa.s to 60,000. Pa.s. According to a further embodiment, the temperature of fluid
  • the main evaporation stage can be operated at a pressure of 100 mbar to 6 bar.
  • the main evaporation stage is a one- or two-shaft kneading apparatus.
  • the main evaporation stage is a single or twin-screw extruder.
  • the main evaporation stage comprises a single process space. There are no process sections along the entire length.
  • the main evaporation stage comprises one or more dome and vapor lines for the removal of volatile compounds. According to another embodiment finds a
  • Self-cleaning effect by applying small amounts of additional solvent to the walls of the main vaporizing cathodes by the condensation of the volatile compounds in the main vaporizing domes or by recirculation to purify them of polymer dust.
  • the viscosity of fluid (D) is in the range of 500 Pa.s to 60,000 Pa.s. According to a further embodiment, the temperature of fluid
  • the degassing stage is operated at a pressure of 100 mbar to 6 bar.
  • the degassing stage is a one- or two-shaft construction, which may be designed as a kneader or extruder.
  • the degassing stage is operated at a pressure of 100 mbar to 6 bar.
  • the degassing stage is a one- or two-shaft construction, which may be designed as a kneader or extruder.
  • the degassing stage is operated at a pressure of 100 mbar to 6 bar.
  • the degassing stage is a one- or two-shaft construction, which may be designed as a kneader or extruder.
  • Degassing kneader a single process room. There are no process sections to recognize the length.
  • the degassing stage comprises one or more dome and vapor lines for the removal of volatile compounds.
  • a self-cleaning effect occurs by applying small amounts of additional solvent to the walls of the main vaporizing domes by the condensation of the volatile compounds in the degassing domes or by recycling them to purify them of polymer dust. According to a further embodiment takes place during the
  • a further embodiment takes place during the degassing an interference of Filier (fillers) or soot, and this filament is subjected during the degassing of a reaction, for example a hydrophobing.
  • the viscosity of fluid (E) is in the range of 500 Pa.s to 10 million Pa.s.
  • the temperature of fluid (E) at the outlet of the degassing stage in the range of 60 ° C to 300 ° C.
  • a special valve is installed at the discharge of the degassing between the pressure increase system and the forming unit, which can completely separate two process sections (Ex / nonEx) and can be discharged with the off-spec products.
  • a shaping aggregate which cuts the polymer into small particles comprises nozzle plates and cutting device or nozzle plate and underwater pelleting means or means for crumbling or turbulators and fixed knives.
  • the shaping unit comprises coolant.
  • the polymer obtains a special strand form through the nozzle construction, which is either cut into blocks or rolled up in the form of skins.
  • the polymer particles are transported pneumatically by means of air in a tube at 10 to 50 m / s.
  • the transport air is actively moistened by adding water with 10 to 200 kg water / t polymer.
  • pneumatically transported granules are heated to about 40 to 70 ° C.
  • a fluid bed dryer is used for tempering.
  • the tempered polymer granules are fed to a shaping, for example a baling press.
  • the polymer molded bodies produced are tested for metal components, weighed, packaged, printed and stored for further processing.
  • a release agent is applied to the
  • Polymer surface applied for example Aerosil or Russl.
  • the vapors of the preconcentration, the main evaporation and the degassing are mixed or separated in a two-stage, depending on the pressure conditions
  • the condensing system is cooled and condensed using industrial cooling water for the first stage and chilled water for the second stage, According to another embodiment, a knock-down vessel is used prior to the first condensation stage.
  • the condensed vapors from the preconcentration are recycled directly without further processing in the previous polymerization process. According to a further embodiment, the condensed
  • a device which comprises the following components:
  • a pre-concentration device comprising one or more stirred or unstirred containers and one
  • a device for main evaporation in particular a first mixing kneader or extruder, and a pressure increasing system, in particular a screw construction or a pump or a combination of screw construction and pump;
  • a degassing device in particular a second mixing kneader or extruder, and a pressure increasing system, in particular a screw design or a pump or a combination of screw design and pump; such as
  • a shaping device comprising a shredding device, for temperature control and a means for packaging and means for pneumatic or hydrodynamic transport.
  • FIG. 1 shows a block diagram of the process according to the invention for the continuous work-up of solution polymers to give polymer moldings
  • Figure 2 is a block diagram representation of an inventive system for the continuous workup of solution polymers to form polymer moldings;
  • Figure 3 is a block diagram representation of a washing stage;
  • FIG. 4-7 block diagrams of different variants of a preconcentration
  • Figure 8 is a block diagram representation of the shape "Direct Baling"
  • Figure 9 is a block diagram representation of the shaping with crushing and pneumatic transport
  • Figure 10 is a block diagram representation of the shaping with underwater granulation.
  • FIG. 11 shows a block diagram of a further exemplary embodiment of the process according to the invention for the continuous preparation of solution polymerization to give polymer moldings
  • Figure 12 is a schematic representation of another embodiment of a plant for carrying out the inventive method
  • Figure 13 is a schematic representation of another embodiment of a system for carrying out the inventive method
  • Figure 14 is a schematic representation of an alternative arrangement of means for performing a pre-concentration
  • Figure 15 is a schematic representation of part of the inventive method, namely the part for the treatment of vapors or a condensation system.
  • a washing step is preceded by a method known from DE 10 2009 007 641 A1 for the direct evaporation of polymers.
  • the corresponding polymers to be processed (fluid A) are first fed to a washing stage 1, in which they are washed with washing liquid.
  • this washing step nonvolatile but soluble components are removed from the polymers.
  • the polymer is preferably mixed with water or another liquid and separated again by the difference in density.
  • the polymer (fluid A) is first fed to a mixer 2 in which it is mixed with washing liquid 3. Thereafter, it passes into a separator 4, are discharged from the washing liquid and the removed components at 5.
  • the purified polymers are fed as fluid B for further treatment.
  • the further treatment is carried out, as described in DE 10 2009 007 641 A1, in a preconcentration stage 6, in which solvent is already removed from the polymer at 7.
  • the preconcentration stage 6 is followed by a main evaporation 8, in which likewise solvent is removed at 9.
  • the now highly viscous or solid polymer is then fed to a shaping stage 13, wherein at 14 also transport aids, as described later, may be effective. Finally, polymer moldings 15 leave this shaping stage 13.
  • the polymer (fluid B) is fed to a polymer solution mixer 16 after the washing stage 1.
  • a heater 17 i.e., substantially heat-treated
  • the polymer enters a vertical flash vessel 18 where it is preconcentrated. This creates vapors of solvent, which are discharged via a discharge 19.
  • a pump 21 is turned on, after which parts of the preconcentrated polymer via a pump 22 again the polymer solution mixer 16 and other parts of a heater 23 (fluid C) are supplied to the preconcentrated polymer.
  • the polymer (fluid B) passes via the reheater 17 directly into the flash container 18, without previously passing through a polymer solution mixer 16 again. Furthermore, the pump 22 presses parts of the preconcentrated polymer via a further heater 24 in the flash tank 18.
  • the variant of an embodiment of the preconcentration shown in FIG. 6 starts with the supply of the polymer (fluid B) from FIG. 5, this polymer (fluid B) via the heater 17 directly into the flash container 18th is entered. Instead of the discharge 20, a mixing kneader 25, in which the already preconcentrated polymer is further treated, then directly adjoins the flash container 18.
  • single-shaft and twin-shaft mixing kneaders are distinguished and used in the present invention.
  • a single-shaft mixing kneader with horizontally arranged shaft is described for example in EP 91 405 497.1.
  • Multi-shaft mixing and kneading machines are described in CH-A 506 322, EP 0 517 068 B, DE 199 40 521 A1 or DE 101 60 535.
  • the flash container is completely omitted and the polymer (fluid B) passes via the reheater 17 directly into the main evaporation, which is formed here by a main steam generator 28, in which the preconcentration also takes place simultaneously.
  • This main exhauster 28 is preferably also a mixing kneader. From it are also withdrawn by a discharge 19 vapors of preconcentration.
  • additives 34 and off-spec material 35 are metered.
  • the largely degassed polymer (fluid E) is fed to the discharge pump 37 of a cutting device (turbulator) 46, in which the polymer is supplied with transport air 47, if necessary, under water 48.
  • a cutting device turbulator
  • Figure 10 is a Underwater granulation shown, wherein the polymer (fluid E) passes after the valve 38 for discharging off-spec material in a cutting device 51, which is designed as an underwater granulator.
  • the granules are treated with transport water 52 and transported to a device for mechanical separation of the water / polymer mixture 53. This can be a sieve. Thereafter, a polymer drying 54, a shaping (baler) 55, a run of the Metal detector 42, a weight test 43, a package 44 and a storage 45th
  • the polymer to be treated is fed as fluid A to the washing stage 1. There, as the arrows indicate, a supply and a discharge of washing liquid. Thereafter, the polymer passes as fluid B in the preconcentration 6. There, a preconcentration according to Figure 5 is indicated. As mentioned above, solvent is evaporated in the preconcentration, which is supplied via the discharge 19 to a condenser 56. The condensate from this passes into a solvent recovery system 57 and from there into a reusable solvent tank.
  • Non-condensable components pass from the condenser 56 under vacuum 58 to a discharge device 59.
  • the polymer passes as fluid C in the main evaporator 8.
  • the solvent evaporated there passes through a discharge device 60 in turn to a condenser 61 and from there to the solvent recovery system 57th
  • the polymer is introduced as fluid D in the degasser 10 and mixed there with appropriate additives 34 and off-spec material.
  • the solvent evaporated in the degasifier 10 is transferred via a line 62 to a further condenser 63, where it is again separated into condensed and non-condensed substances.
  • the non-condensed gases are fed by vacuum 64 to the purge device 59, while the condensate is again supplied to a solvent-water separation device 65 and thereafter the separated solvent recovery solvent 57.
  • the process according to FIG. 9 is shown, in which the polymer comminuted in a turbulator is conveyed to the next processing stages with transport air.
  • FIG. 11 shows the possible sequences of a further exemplary embodiment of the method according to the invention.
  • the fluid B which consists of a volatile compound having a non-volatile polymer content of 2 to 35 wt .-%, is input to a pre-concentration stage 6.
  • the fluid B is preconcentrated to a fluid C.
  • this fluid C has a polymer content of 25-70 wt .-%, it is fed to a main evaporation 8, in which the volatile compounds are further evaporated. This gives the product a polymer content of 90-95 wt .-% and leaves as fluid D, the main evaporation. It is then fed to a degassing 10, in which a degassing to a polymer content of 95-99.99 wt .-% takes place.
  • the main evaporation 8 can be skipped and the fluid can be fed directly to the degasification 10. Again, the degassed product leaves the degassing as fluid E with a polymer content of 95-99.99 wt .-%. This fluid E is then fed to a mold 13 in which it is finished up to the final product, that is, to the mold body 15.
  • the fluid B is introduced via a pump 74.1 and a heating device 77.1 into a flash tank 75 (ie, injected under a pre-pressure).
  • a flash tank 75 ie, injected under a pre-pressure.
  • this flash tank 75 a pre-concentration, wherein a part of the volatile components via a Brüden Gustav 78.1 subtracted and further treated, as described in particular to Figure 15.
  • the preconcentrated product is discharged as a fluid C by means of a gear pump 81 from the flash tank 75.
  • a portion of the fluid C is returned via a further pump 74.2 via the heater 77.1 back into the flash tank 75.
  • Another part of the fluid C is fed via a heating device 77.2 of the main evaporation 8, which consists essentially of a mixing kneader 71.1. Mixing elements in this mixing kneader 71.1 are set in motion by a drive 76.1.
  • the main vaporized product leaves via a discharge 72.1, preferably a discharge screw, the mixing kneader 71.1 and passes as fluid D in an extruder 71.2 in the degassing 10.
  • a screw in this extruder 71.2 is rotated by another drive 76.2 in rotary motion.
  • a further cylinder dome 73.2 sits on the extruder 71.2, to which a further vapor line 78.3 connects, which likewise leads to the condensation system according to FIG.
  • the degassed product leaves as fluid E the extruder 71.2 via another discharge 72.2, in particular a discharge screw.
  • the exemplary embodiment of the installation for carrying out the method according to the invention according to FIG. 13 differs from that according to FIG. 12 in that the heating device 77.2 connects directly to the flash tank 75 or the gear pump 81 and only thereafter Subsequently, a portion of the fluid C via the pump 74.2 and the heater 77.1 back into the flash tank 75 is performed.
  • FIG. 14 shows a further exemplary embodiment of the preconcentration 6.
  • the fluid B passes through a heat exchanger 82 and the heater 77.1 in the flash tank 75.
  • a vapor line 78.4 leads back to the heat exchanger 82, where a portion of the vapors via the heater 77.1 is fed back into the flash tank 75.
  • Another part of the vapors is discharged, in particular fed to the condensation system shown in Figure 15.
  • the first flash tank 75 serves for a first preconcentration, the preconcentrated fluid being introduced via the gear pump 81 and a further heating device 77.2 into a further flash tank 75.1. Vapors from this further flash tank 75.1 are in turn fed via a vapor line 78.2 to the condensation system shown in FIG.
  • the now preconcentrated fluid C leaves the second flash tank 75.1 via the gear pump 81.1. Part of this, as described for FIG. 12, is led back to the flash tank 75.1 via the pump 74.3 and the heater 77.2, another part passes into the main evaporation 8 or, since in the present case a stronger preconcentration takes place directly into the degasification 10th
  • the vapors arrive via the various vapor lines first in a first condenser 79, in which industrial water is used as cooling water. From this capacitor takes place once a discharge of condensed vapor components, in particular of polymer components to a collector 82, while the volatile components are fed to a second capacitor 80.
  • This second condenser is preferably operated with chilled water.
  • the condensed Fluid components are also supplied from this second condenser 80 to the collector 82, while the volatile gas components are withdrawn via a pump 74.4 and discharged.
  • the fluid components from the collector 82 are recycled via a pump 74.5.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Dispersion Chemistry (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)

Abstract

L'invention concerne un dispositif et un procédé de traitement de produits de polymérisation en solution pour obtenir des éléments moulés en polymère, comprenant une étape de lavage en amont, à laquelle est amené le polymère/produit de polymérisation avant le traitement; un moyen de pré-concentration (6) comprenant un ou plusieurs récipients (75) et éventuellement un moyen de recirculation; un moyen d'évaporation principale (8), notamment un premier pétrisseur-mélangeur (71.1), et un système élévateur de pression, notamment une construction à vis (72.1) ou une pompe ou une combinaison d'une construction à vis et d'une pompe; un moyen de dégazage (10), notamment un second pétrisseur-mélangeur(71.2), et un système élévateur de pression, notamment une construction à vis (72.2) ou une pompe ou une combinaison de d'une construction à vis et d'une pompe; et un moyen de formage (13), comprenant un moyen de fractionnement, de commande de température et d'emballage et de préférence un moyen de transport pneumatique; un moyen de condensation des vapeurs de préférence comportant un système à dépression monté en aval; et un moyen de fonctionnement, de commande et de régulation de tout le processus.
PCT/EP2014/002240 2013-08-15 2014-08-15 Procédé et dispositif de transformation de polymères/produits de polymérisation en solution en éléments moulés en polymère WO2015022079A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102013108845 2013-08-15
DE102013108845.7 2013-08-15
DE102014108627.9 2014-06-18
DE102014108627 2014-06-18

Publications (1)

Publication Number Publication Date
WO2015022079A1 true WO2015022079A1 (fr) 2015-02-19

Family

ID=51585063

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2014/002240 WO2015022079A1 (fr) 2013-08-15 2014-08-15 Procédé et dispositif de transformation de polymères/produits de polymérisation en solution en éléments moulés en polymère

Country Status (1)

Country Link
WO (1) WO2015022079A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016030467A3 (fr) * 2014-08-27 2016-05-12 List Holding Ag Procédé pour améliorer l'isolation de solutions polymères
WO2017034685A1 (fr) * 2015-08-25 2017-03-02 Exxonmobil Chemical Patents Inc. Système de réacteur pour procédé de polymérisation multi-phase
WO2017108963A1 (fr) * 2015-12-21 2017-06-29 Borealis Ag Procédé de récupération d'hydrocarbures dans un processus de polymérisation en solution
CN107553767A (zh) * 2017-10-10 2018-01-09 广东普赛达密封粘胶有限公司 一种连续化湿固化聚氨酯组合物生产线及其生产方法
CN110733144A (zh) * 2019-10-29 2020-01-31 六安正辉优产机电科技有限公司 用于塑料泡沫回收利用的熔融造粒工艺

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH506322A (de) 1969-03-17 1971-04-30 List Heinz Mehrspindelige Misch- und Knetmaschine
EP0262594A2 (fr) * 1986-10-01 1988-04-06 Polysar Limited Récupération d'un polymère d'une solution
EP0517068B1 (fr) 1991-06-07 1995-09-06 List Ag Pétrisseur de mélange
DE19537113C1 (de) * 1995-10-05 1997-03-13 Bayer Ag Verfahren zur Herstellung von thermoplastischem Polymergranulat aus Polymerlösungen
DE19940521A1 (de) 1999-08-26 2001-04-19 List Ag Arisdorf Mischkneter
JP2002161109A (ja) * 1999-10-12 2002-06-04 Kanegafuchi Chem Ind Co Ltd イソブチレン系ブロック共重合体樹脂溶液からの有機溶媒除去方法及びペレット製造方法
DE10160535A1 (de) 2001-12-10 2003-06-18 List Ag Radial oder axial reinigende Mischbarren
WO2010089137A2 (fr) * 2009-02-05 2010-08-12 List Holding Ag Procédé et dispositif de traitement continu de mélanges de substances
DE102009007641A1 (de) 2009-02-05 2010-08-19 List Holding Ag Verfahren und Vorrichtung zur kontinuierlichen Behandlung von Stoffgemischen
CH702321B1 (de) * 2006-05-12 2011-06-15 List Holding Ag Verfahren zur kontinuierlichen Direkteindampfung und Entgasung von Lösungsmittel, Monomer, Katalysator-, Initiator- oder Reaktionsresten aus der Polymerisation von temperaturempfindlichen, elastomerhaltigen Polymerlösungen.
DE102009061077A1 (de) * 2009-02-05 2011-06-22 List Holding Ag Verfahren zur kontinuierlichen Behandlung eines zähviskosen, pastösen Produktes
US20120043687A1 (en) * 2008-09-19 2012-02-23 Lanxess International Sa Process for the production of water and solvent-free polymers
US20130203943A1 (en) * 2010-03-24 2013-08-08 Lanxess International Sa Process for the production of water and solvent-free halobutyl rubbers

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH506322A (de) 1969-03-17 1971-04-30 List Heinz Mehrspindelige Misch- und Knetmaschine
EP0262594A2 (fr) * 1986-10-01 1988-04-06 Polysar Limited Récupération d'un polymère d'une solution
EP0517068B1 (fr) 1991-06-07 1995-09-06 List Ag Pétrisseur de mélange
DE19537113C1 (de) * 1995-10-05 1997-03-13 Bayer Ag Verfahren zur Herstellung von thermoplastischem Polymergranulat aus Polymerlösungen
DE19940521A1 (de) 1999-08-26 2001-04-19 List Ag Arisdorf Mischkneter
JP2002161109A (ja) * 1999-10-12 2002-06-04 Kanegafuchi Chem Ind Co Ltd イソブチレン系ブロック共重合体樹脂溶液からの有機溶媒除去方法及びペレット製造方法
DE10160535A1 (de) 2001-12-10 2003-06-18 List Ag Radial oder axial reinigende Mischbarren
CH702321B1 (de) * 2006-05-12 2011-06-15 List Holding Ag Verfahren zur kontinuierlichen Direkteindampfung und Entgasung von Lösungsmittel, Monomer, Katalysator-, Initiator- oder Reaktionsresten aus der Polymerisation von temperaturempfindlichen, elastomerhaltigen Polymerlösungen.
US20120043687A1 (en) * 2008-09-19 2012-02-23 Lanxess International Sa Process for the production of water and solvent-free polymers
WO2010089137A2 (fr) * 2009-02-05 2010-08-12 List Holding Ag Procédé et dispositif de traitement continu de mélanges de substances
DE102009007641A1 (de) 2009-02-05 2010-08-19 List Holding Ag Verfahren und Vorrichtung zur kontinuierlichen Behandlung von Stoffgemischen
DE102009061077A1 (de) * 2009-02-05 2011-06-22 List Holding Ag Verfahren zur kontinuierlichen Behandlung eines zähviskosen, pastösen Produktes
US20130203943A1 (en) * 2010-03-24 2013-08-08 Lanxess International Sa Process for the production of water and solvent-free halobutyl rubbers

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016030467A3 (fr) * 2014-08-27 2016-05-12 List Holding Ag Procédé pour améliorer l'isolation de solutions polymères
WO2017034685A1 (fr) * 2015-08-25 2017-03-02 Exxonmobil Chemical Patents Inc. Système de réacteur pour procédé de polymérisation multi-phase
US10717063B2 (en) 2015-08-25 2020-07-21 Exxonmobil Chemical Patents Inc. Reactor system for multi-phase polymerization process
WO2017108963A1 (fr) * 2015-12-21 2017-06-29 Borealis Ag Procédé de récupération d'hydrocarbures dans un processus de polymérisation en solution
KR20180082573A (ko) * 2015-12-21 2018-07-18 보레알리스 아게 용액 중합 공정에서의 탄화수소 회수 공정
CN108602900A (zh) * 2015-12-21 2018-09-28 博里利斯股份公司 一种用于在溶液聚合过程中回收烃的方法
KR102051767B1 (ko) 2015-12-21 2019-12-03 보레알리스 아게 용액 중합 공정에서의 탄화수소 회수 공정
US10759880B2 (en) 2015-12-21 2020-09-01 Borealis Ag Process for recovering hydrocarbons in a solution polymerisation process
CN108602900B (zh) * 2015-12-21 2021-01-05 博里利斯股份公司 一种用于在溶液聚合过程中回收烃的方法
CN107553767A (zh) * 2017-10-10 2018-01-09 广东普赛达密封粘胶有限公司 一种连续化湿固化聚氨酯组合物生产线及其生产方法
CN110733144A (zh) * 2019-10-29 2020-01-31 六安正辉优产机电科技有限公司 用于塑料泡沫回收利用的熔融造粒工艺
CN110733144B (zh) * 2019-10-29 2021-05-28 常州中科绿塑环保科技有限公司 用于塑料泡沫回收利用的熔融造粒工艺

Similar Documents

Publication Publication Date Title
AT410942B (de) Verfahren und vorrichtung zur erhöhung der grenzviskosität von polyester
EP2001585B1 (fr) Procédé et dispositif pour la mise en oeuvre des procedes de polymerisation
WO2015022079A1 (fr) Procédé et dispositif de transformation de polymères/produits de polymérisation en solution en éléments moulés en polymère
AT411161B (de) Verfahren und vorrichtung zum recyclen von pet-gut
EP2021116B1 (fr) Procédé et dispositif de recyclage de matériau polyester
EP1425145B1 (fr) Procede et dispositif pour la production des melanges elastomeres pour la production de caoutchouc
EP2029267B1 (fr) Procédé et dispositif de polymérisation en continu d'un polymère en phase solide
DE19641781A1 (de) Verfahren und Vorrichtung zum gleichzeitigen Mahlen und Trocknen eines feuchten Celluloseether enthaltenden Mahlgutes
WO2010089137A2 (fr) Procédé et dispositif de traitement continu de mélanges de substances
EP2831198A1 (fr) Dispositif et procédé de dépolymérisation catalytique d'une matière contenant un hydrocarbure
CH717294A1 (de) Verfahren zur Geruchsentfernung aus recycelten Polyolefin-Pellets.
DE102018102811A1 (de) Extruder, Anlage mit einem Extruder, Verfahren zur Herstellung von Zielpolymerprodukten aus einem kunststoffhaltigen Material aus einer Lösung unter Verwendung eines solchen Extruders
EP1078698B1 (fr) Procédé et dispositif pour le traitement thermolytique des matières contenant des polymères et de la cellulose, notamment des produits déchiquetés légèrs
EP2450098A1 (fr) Procédé de mélange d'un produit mélangé constitué de particules de matière solide et agencement de mélangeur
WO2010099963A1 (fr) Procédé et dispositif de dépolymérisation continue ou discontinue de polycaprolactame
WO2008145474A2 (fr) Procédé et dispositif de décomposition thermique d'une matière de base au moyen de particules étrangères
EP1382425B1 (fr) Procédé de réalisation de mélanges de caoutchoucs
DE19522164A1 (de) Verfahren und Vorrichtung zur kontinuierlichen Trocknung von Protein enthaltendem Schlamm
CH702321B1 (de) Verfahren zur kontinuierlichen Direkteindampfung und Entgasung von Lösungsmittel, Monomer, Katalysator-, Initiator- oder Reaktionsresten aus der Polymerisation von temperaturempfindlichen, elastomerhaltigen Polymerlösungen.
WO2016030467A2 (fr) Procédé pour améliorer l'isolation de solutions polymères
DE858896C (de) Verfahren zur Herstellung olefinischer Elastomerer
EP2253693A1 (fr) Procédé de traitement de matières résiduelles de brasseries
DE102009007641A1 (de) Verfahren und Vorrichtung zur kontinuierlichen Behandlung von Stoffgemischen
DE102009061077A1 (de) Verfahren zur kontinuierlichen Behandlung eines zähviskosen, pastösen Produktes
EP1738661B1 (fr) Procédé de fabrication de produits alimentaires intermédiaires et/ou de mélanges alimentaires pour animaux et dispositif correspondant

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14771506

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 14771506

Country of ref document: EP

Kind code of ref document: A1