WO2002004190A1 - Procede et dispositif de production de mousses - Google Patents

Procede et dispositif de production de mousses Download PDF

Info

Publication number
WO2002004190A1
WO2002004190A1 PCT/EP2001/007214 EP0107214W WO0204190A1 WO 2002004190 A1 WO2002004190 A1 WO 2002004190A1 EP 0107214 W EP0107214 W EP 0107214W WO 0204190 A1 WO0204190 A1 WO 0204190A1
Authority
WO
WIPO (PCT)
Prior art keywords
line
blowing agent
mixer
reaction
jump
Prior art date
Application number
PCT/EP2001/007214
Other languages
German (de)
English (en)
Inventor
Hans-Michael Sulzbach
Ferdinand Althausen
Reiner Raffel
Martin Schamberg
Original Assignee
Hennecke Gmbh
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 Hennecke Gmbh filed Critical Hennecke Gmbh
Priority to AU2001283887A priority Critical patent/AU2001283887A1/en
Publication of WO2002004190A1 publication Critical patent/WO2002004190A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3442—Mixing, kneading or conveying the foamable material

Definitions

  • the invention relates to a method and a device for producing foams from at least two reacting liquid reaction components, wherein at least one of these reaction components powdery, fibrous or fine-grained additives and at least one of these reaction components admixed with a blowing agent which changes from the liquid to the gaseous state in the event of a corresponding pressure jump become.
  • foams in particular from polyurethane, by reacting polyol with isocyanate.
  • the blowing agents for cell formation are those which are in a liquid state under the appropriate pressure, but which, when relaxed, change to a gaseous state as a result of a pressure jump of a corresponding height and are then available as cell gas when the reaction mixture is foamed.
  • Carbon dioxide in particular has proven its worth in terms of environmental compatibility.
  • a discharge device arranged behind the reaction mixer and designed accordingly serves to generate the pressure jump or the necessary relaxation.
  • sieves with a suitable mesh size, perforated plates, splitting elements, sintered metal plates, ball beds or the like are suitable, i.e. Organs which exert such a pressure jump on the propellant-laden reaction mixture as it flows through, through which the propellant changes from the liquid to the gaseous state.
  • Such discharge organs have been launched on the market under the terms "Creamer” and "Lay-down device”.
  • the density of the liquid foam is further reduced by water added to the polyol component, which forms CO2 on reaction with isocyanate.
  • the invention preferably relates to the production of polyurethane foams from polyol and isocyanate, but is also for the production of others
  • Fine-grained additives usually consist of melamine, activated carbon, chalk, calcium carbonate, heavy spar; powdery e.g. from graphite powder, ammonium polyphosphate or recycled powder; fibrous preferably made of glass, aramid or plastics, in particular polypropylene fibers.
  • Suitable powdered fillers typically have grain sizes of approximately 10 to 50 ⁇ m. Fibrous fillers preferably have a diameter of 6 to 14 ⁇ m and a length of 100 to 200 ⁇ m. It has been shown that such
  • fillers are preferably used in an amount of 10 to 40% by weight, based on the finished foam, i.e. that the polyol filler dispersion has between about 20 and 50 wt .-% filler.
  • the fillers are preferably dispersed in the polyol component by means of conventional stirrers and dispersers with conveyance into or into the storage tank.
  • the storage tank is preferably stirred to prevent the fillers from settling.
  • the same reaction component serves as a carrier for the additive and blowing agent.
  • reaction component loaded with additive is diluted again by adding the liquid blowing agent.
  • one branch of a reactant additive and the other branch of blowing agent can also be mixed in, and then both loaded branches of the reactant are premixed with one another before they are mixed with the second reactant.
  • One branch of the reactant can also be loaded with aggregate and the other branch with blowing agent, but then the two are loaded Branches of the reaction component are fed separately to the second reaction component and mixed therewith.
  • the addition of the additives and the blowing agent can be better controlled because they are not fed into the same component stream.
  • additive and / or blowing agent can be carried out online during production, it is preferred to generate a batch (storage tank) beforehand from the reaction component and additive.
  • the pre-dispersion presented or generated online in the storage tank is then subjected to agglomerate cleavage by means of high shear rates and, if necessary, impact forces.
  • the agglomerate clump rank takes place on-line during the supply of the dispersion to the main mixer and / or in the "conditioning mode" in a circulation line from the storage tank and back into it.
  • the agglomerate clump is at least on-line, possibly additionally in the "conditioning mode".
  • the shear rates to which the pre-dispersion is subjected during the agglomerate cleavage are preferably more than 10 5 s -1 .
  • Shear rates above 3'10 5 s _1 are particularly preferred.
  • the shear rate is generated by providing at least one perforated orifice in the feed line to the main mixer and / or the circulation line, through which the pre-dispersion under a high admission pressure of preferably 20 to 150 bar, particularly preferably 30 to 80 bar, more preferably 30 up to 50 bar.
  • Shear rate in the sense of the invention is to be understood to mean 3 times the average passage speed of the dispersion divided by the radius of the pinhole.
  • the at least one pinhole preferably has a diameter of not less than 0.5 mm, preferably between 1 and 1.5 mm. With diameters above
  • perforated orifices are parallel, i.e. flowed through from the same form to be provided.
  • a perforated plate with 4 to 10 perforated screens with a diameter of 2 mm or with 10 to 25 perforated screens with a 1.5 mm diameter or with 25 to 50 perforated screens with 1 mm diameter.
  • two or three perforated plates can be used one behind the other in the direction of flow, since the pressure required to achieve a sufficient shear rate is smaller with a smaller aperture diameter.
  • two perforated screens are arranged opposite each other and flowed through in the opposite direction, so that the dispersion jets emerging from the perforated screens collide with one another.
  • Such apparatuses are known in principle, for example, from EP-A 685 544 and WO 01/05517 for droplet dispersion in coating production.
  • FIG. 3 shows an exemplary embodiment with feed of additive in a first polyol component and feed of the blowing agent in a second polyol component and subsequent premixing of both polyols
  • FIG. 4 shows an exemplary embodiment analogous to FIG. 3 with the difference that both polyols open separately into the mixer
  • FIG. 6 shows a further embodiment of the agglomerate crusher.
  • the device consists of a batch container 1, in which one
  • Storage container 2 via a line 4 provided with a pump 3 polyol and from a storage container 5 as an additive melamine via a with a metering
  • Snail 6 provided line 7 are introduced.
  • the batch is created using a Agitator 8 generated.
  • a line 9 opens, which leads via a metering pump 10, a shut-off valve 11, a filter 12, a mixer 13 and a pressure relief valve 14 into a main mixer 15 designed as an agitator mixer.
  • a circuit line 16 branches off in front of the shutoff valve 11 and leads back into the batch container 1 via a shutoff valve 17 and an agglomerate shredder 18 according to the invention.
  • a storage container 19 contains carbon dioxide as a blowing agent.
  • a line 20 leads from it via a pump 21 and opens into the line 9 between the filter 12 and the mixer 13.
  • a line 24 leads from a storage container 22 for isocyanate as the second reaction component via a metering pump 23 and opens into the main mixer 15 on. Inlets 25 for further additives are provided on the main mixer 15. The main mixer 15 is followed by an outlet element 26 which produces a jump in the propellant.
  • the device consists of a batch container 31, in which one
  • Storage containers 32 are introduced via a line 34 provided with a pump 33 polyol and from a storage container 35 as additive melamine via a line 37 provided with a metering screw 36.
  • the batch is generated by means of an agitator 38.
  • a line 39 opens from the batch container 31 and leads via a metering pump 40, an agglomerate chopper 41, a shut-off valve 42 and a filter 43 into a main mixer 44 designed as an agitator mixer.
  • the agglomerate shredder 41 can be adapted to different additives by means of a drain indicator 57 and a control device 58. Between the agglomerate shredder 41 and the shut-off valve 42, a circuit line 46 containing a shut-off valve 45 branches off from the line 39 and which flows into the
  • a storage container 47 contains carbon dioxide as a blowing agent.
  • a line 48 leads from it via a pump 49 and opens between a metering pump 50 and a mixer 51 into a line 52. This leads from a reservoir 53 for isocyanate and opens into the main mixer 44 via a throttle 54 arranged downstream of the mixer 51. Inlets 55 for further additives are provided on the main mixer 44.
  • the main mixer 44 is one Subsequent pressure jump in the blowing agent generating outlet member 56.
  • the pump 40 provides such a pressure that the dissolved carbon dioxide in the main mixer 44 does not change to the gaseous state and there is also a sufficiently large pressure difference above the agglomerate shredder for the agglomerate clump.
  • the device Before the start of production, the device is preferably operated for a few hours in the "conditioning mode" with the valve 42 and the valve 45 open and in the "on-line mode" during production with the valve 42 open and the valve 45 closed.
  • the device consists of a batch container 61, in which one
  • Storage containers 62 are introduced via a line 64 provided with a pump 63, and a first polyol is introduced from a storage container 65 as an additive melamine via a line 67 provided with a dosing screw 66.
  • the batch is generated by means of an agitator 68.
  • a line 69 opens out from the batch container 61, said line 69 via a metering pump 70, a shut-off valve 71, a filter 72
  • a circuit line 76 branches off before the shut-off valve 71, which leads back into the batch container 61 via a shut-off valve 77 and an agglomerate shredder 78. Carbon dioxide is contained as a blowing agent in a storage container 79.
  • a line 80 leads from it via a pump 81 and merges with a line 82, which leads via a metering pump 83 from a reservoir 84 for a second polyol.
  • the combined line 85 then leads via a mixer 86 and a throttle 87 between the filter 72 and the mixer 73 into the line 69.
  • a line 90 leads from a reservoir 88 for isocyanate via a metering pump 89 and opens into the main mixer 75.
  • the device consists of a batch container 101, into which a first polyol is introduced from a storage container 102 via a line 104 provided with a pump 103 and from a storage container 105 as an additive melamine via a line 107 provided with a metering screw 106.
  • the batch is generated by means of an agitator 108.
  • a line opens from the batch container 101
  • agglomerate shredder 111 which leads via a metering pump 110, an agglomerate chopper 111, a shut-off valve 112 and a filter 113 into a main mixer 114 designed as an agitator mixer.
  • the agglomerate shredder 111 can be adapted to different aggregates by means of a drain indicator 131 and a control device 132. Between agglomerate shredder 111 and shut-off valve
  • a circuit line 116 containing a shut-off valve 115 branches off from line 109, a circuit line 116 containing a shut-off valve 115, which leads back into the batch container 101.
  • a storage container 117 contains carbon dioxide as a blowing agent.
  • a line 118 leads from it via a pump 119 and merges with a line 120 to form a line 121.
  • the line 120 leads via a dose umpe 122 from a storage container 123 for a second polyol.
  • a mixer 124 and a throttle 125 are arranged in the combined line 121; it opens into the main mixer 114.
  • a line 127 discharging from a reservoir 126 for isocyanate flows into this main mixer 114 via a metering pump 128.
  • Inlets 129 for further additives are provided on the main mixer 114. It is followed by an outlet member 130 that produces a jump in the propellant.
  • the jump in pressure is designed by the choice of the flow cross-section of the discharge member 130 such
  • Fig. 5 shows an agglomerate shredder according to the invention, which consists of a transverse to
  • FIG. 6 shows an agglomerate shredder designed as an installation 602 in a pipe section 601, in which the respective opposing (preferably sharp-edged) Holes are provided through which the polyol filler dispersion is pressed so that the dispersion jets emerging from opposite holes collide with one another.

Landscapes

  • Polyurethanes Or Polyureas (AREA)

Abstract

La présente invention concerne des mousses produites à partir de substances réactionnelles pouvant s'écouler auxquelles est ajoutée une charge d'une part d'un granulat poudreux, finement particulaire ou fibreux, et d'autre part d'un agent moussant qui, lors de son passage au niveau d'un organe de sortie (26) disposé en aval d'un mélangeur (principal) (15), passe de l'état liquide à l'état gazeux. Selon la présente invention, lors de la production de ces mousses, l'obstruction dudit organe de sortie (26) peut être évitée grâce à la destruction des agglomérés formés, au moyen d'un système de fractionnement d'agglomérés (18) disposé entre le point d'alimentation du granulat et l'organe de sortie (26).
PCT/EP2001/007214 2000-07-07 2001-06-25 Procede et dispositif de production de mousses WO2002004190A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2001283887A AU2001283887A1 (en) 2000-07-07 2001-06-25 Method and device for producing foams

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10033068.1 2000-07-07
DE10033068 2000-07-07

Publications (1)

Publication Number Publication Date
WO2002004190A1 true WO2002004190A1 (fr) 2002-01-17

Family

ID=7648135

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2001/007214 WO2002004190A1 (fr) 2000-07-07 2001-06-25 Procede et dispositif de production de mousses

Country Status (2)

Country Link
AU (1) AU2001283887A1 (fr)
WO (1) WO2002004190A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1464464A2 (fr) * 2003-03-18 2004-10-06 Hennecke GmbH Procédé pour la préparation de mousses de polyuréthane
CN114437397A (zh) * 2020-10-16 2022-05-06 中国石油化工股份有限公司 发泡珠粒的发泡装置及生产方法与应用、发泡珠粒

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4442254A1 (de) * 1994-11-28 1996-05-30 Hennecke Gmbh Maschf Verfahren und Vorrichtung zur Schaumherstellung mittels unter Durck gelöstem Kohlendioxid
EP0794857A1 (fr) * 1994-11-28 1997-09-17 Bayer Ag Procede et dispositif de production de mousse a l'aide de dioxyde de carbone dissous sous pression
US5801210A (en) * 1997-10-29 1998-09-01 Bayer Corporation Method and apparatus for the production of essentially void free foams
EP0878284A2 (fr) * 1997-05-05 1998-11-18 Hennecke GmbH Procédé et dispositif pour la production de mousse polyuréthane utilisant du CO2 comme agent gonflant

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4442254A1 (de) * 1994-11-28 1996-05-30 Hennecke Gmbh Maschf Verfahren und Vorrichtung zur Schaumherstellung mittels unter Durck gelöstem Kohlendioxid
EP0794857A1 (fr) * 1994-11-28 1997-09-17 Bayer Ag Procede et dispositif de production de mousse a l'aide de dioxyde de carbone dissous sous pression
EP0878284A2 (fr) * 1997-05-05 1998-11-18 Hennecke GmbH Procédé et dispositif pour la production de mousse polyuréthane utilisant du CO2 comme agent gonflant
US5801210A (en) * 1997-10-29 1998-09-01 Bayer Corporation Method and apparatus for the production of essentially void free foams

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1464464A2 (fr) * 2003-03-18 2004-10-06 Hennecke GmbH Procédé pour la préparation de mousses de polyuréthane
EP1464464A3 (fr) * 2003-03-18 2006-06-21 Hennecke GmbH Procédé pour la préparation de mousses de polyuréthane
CN114437397A (zh) * 2020-10-16 2022-05-06 中国石油化工股份有限公司 发泡珠粒的发泡装置及生产方法与应用、发泡珠粒

Also Published As

Publication number Publication date
AU2001283887A1 (en) 2002-01-21

Similar Documents

Publication Publication Date Title
DE4316190C1 (de) Verfahren und Vorrichtung zum Aufbereiten von Polyurethanschaumstoff-Abfällen, insbesondere Weichschaumstoff-Abfällen, zur Wiederverwertung als Zuschlagstoffe bei der Polyurethanherstellung
EP0907478B1 (fr) Procede pour la production de mousse a l'aide de dioxyde de carbone dissous sous pression
EP1539453B1 (fr) Procede de production de mousse polyurethane exempte de poches et de trous d'epingle
EP1299443B1 (fr) Procede de production d'une plaque de mousse
DE1694621A1 (de) Verfahren zur Herstellung von gegebenenfalls verschaeumten Urethangruppen aufweisenden Kunststoffen
EP0960008B1 (fr) Procede et dispositif permettant de produire du polyurethanne contenant des matieres de remplissage
EP1464464B1 (fr) Procédé et appareil pour la préparation de mousses de polyuréthane
WO2002004190A1 (fr) Procede et dispositif de production de mousses
WO2017157534A1 (fr) Procédé pour préparer des dispersions ayant une taille de particules définie
EP0878284B1 (fr) Procédé et dispositif pour la production de mousse polyuréthane utilisant du CO2 comme agent moussant
WO1999043478A1 (fr) Procede pour la production de matieres moussantes, notamment de matieres cimentaires moussantes, et dispositif a cet effet
WO1996002377A1 (fr) Procede et dispositif pour la production de mousses au moyen de dioxyde de carbone dissous sous pression
WO2003064236A1 (fr) Procede pour la production de mousse polyurethanne a structure cellulaire ajustable
EP2931840B1 (fr) Procédé et installation permettant de préparer une mousse de liant destinée à la fabrication d'asphalte
EP0379015B1 (fr) Procédé pour charger au moins un composant avec du gaz dans la fabrication des matières plastiques massives ou cellulaires
DE102022117527A1 (de) System und Verfahren zur Herstellung von brandhemmendem Schaumstoff
EP1198287A1 (fr) Procede et dispositif pour produire des mousses, en particulier des matieres legeres poreuses moussees
EP0804328A1 (fr) Procede et dispositif pour la production de mousses au moyen de dioxyde de carbone dissous sous pression
DE102015120526B4 (de) Vorrichtung und Verfahren zur Aufbereitung eines flüssigen Polymergemisches
WO2022135714A1 (fr) Appareil de production de béton enrichi en co2
DE19718895C1 (de) Verfahren und Vorrichtung zur Herstellung von Polyurethan-Schaum mittels flüssigem Kohlendioxid als Schäummittel
DE102004018436A1 (de) Verfahren sowie Vorrichtung zur Bereitstellung eines Polymer-Granulats
DE3404313C2 (de) Verfahren zum Mischen disperser Feststoffe nach dem Schwerkraftprinzip
EP3560580A1 (fr) Installation et procédé de fabrication d'un mélange de bitume
DE2750938A1 (de) Dosier- und mischvorrichtung zur herstellung von kunststoffen insbesondere gefuellten polyurethanschaeumen

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: FESTSTELLUNG EINES RECHTSVERLUSTS NACH REGEL 69(1) EPUE

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP