[go: up one dir, main page]

WO2008116575A1 - Procédé et dispositif pour la production d'éléments isolants - Google Patents

Procédé et dispositif pour la production d'éléments isolants Download PDF

Info

Publication number
WO2008116575A1
WO2008116575A1 PCT/EP2008/002144 EP2008002144W WO2008116575A1 WO 2008116575 A1 WO2008116575 A1 WO 2008116575A1 EP 2008002144 W EP2008002144 W EP 2008002144W WO 2008116575 A1 WO2008116575 A1 WO 2008116575A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactive component
pump
metering
reactive
premixer
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2008/002144
Other languages
German (de)
English (en)
Inventor
Jürgen Wirth
Dietmar Dreher
Ulrich Knapp
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hennecke GmbH
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
Publication of WO2008116575A1 publication Critical patent/WO2008116575A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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
    • B29C44/3446—Feeding the blowing agent
    • 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
    • B29B7/002—Methods
    • B29B7/007—Methods for continuous mixing
    • 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
    • B29B7/32—Mixing; Kneading continuous, with mechanical mixing or kneading devices with non-movable mixing or kneading devices
    • B29B7/325—Static 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
    • B29B7/76—Mixers with stream-impingement mixing head
    • B29B7/7615—Mixers with stream-impingement mixing head characterised by arrangements for controlling, measuring or regulating, e.g. for feeding or proportioning the components
    • B29B7/7621—Mixers with stream-impingement mixing head characterised by arrangements for controlling, measuring or regulating, e.g. for feeding or proportioning the components involving introducing a gas or another component in at least one of the components
    • 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
    • B29C44/60—Measuring, controlling or regulating

Definitions

  • the invention relates to a method and a device for producing insulating elements of polyurethane (PUR) or polyisocyanurate (PIR) foam, in which the blowing agent is mixed in a circulation in at least one of the two reactive components.
  • PUR polyurethane
  • PIR polyisocyanurate
  • the production of insulating elements for thermal insulation of PUR or PIR foam is generally carried out in a continuous process.
  • the insulation elements are produced endlessly on so-called contimates in thicknesses of generally about 20 to 200 mm. Thicknesses of less than 20 mm or over 200 mm are also possible.
  • Such a Contimat usually consists of a circumferential upper belt for guiding the upper cover layer, a circumferential lower belt for guiding the lower cover layer, a feed device for the upper cover layer, a feed device for the lower cover layer, a molding section, within which the reaction mixture between the upper cover layer and the lower cover layer is foamed and reacted, a cutting device for the insulating elements to be produced and a dosing station with a mixing head for applying the reactive mixture to the lower cover layer.
  • a Contimat according to the prior art is shown in FIG.
  • the reactive mixture is formed by mixing an A-reactive component with a B-reactive component, wherein the A-reactive component includes at least one polyether or a polyester polyol or mixtures of polyether and polyester polyols and the B-reactive component at least one isocyanate or Isocyanatabmischept. Furthermore, in the A-reactive component or in the B-reactive component or proportionately in both the A and the B-reactive component nor a halogen-free blowing agent, e.g. Pentane, as well as PUR or PIR foam specific additives mixed.
  • a halogen-free blowing agent e.g. Pentane
  • PIR systems are highly reactive. This has the consequence that a traversing of the mixing head to apply the mixture is not possible because the individual webs no longer flow together.
  • a traversing of the mixing head to apply the mixture is not possible because the individual webs no longer flow together.
  • PIR foams are extremely temperature critical. This requires an exact temperature control for the reactive components. In order to achieve an optimal process flow, therefore, amounts of heat introduced by process organs should, as far as possible, be removed directly behind the heat input point. This also means that process agents that introduce less heat into the reactive components than others that otherwise perform the same function are the more appropriate.
  • Polyurethane polyols are generally used in PUR systems and highly viscous polyester polyols in PIR systems, the viscosity of which can be up to 10,000 mPas.
  • foaming agent required for the foaming process, based on the polyol, for example, about 16 to 25 parts by weight of pentane, but only go to a small proportion, namely only about 3 to 5 parts by weight in solution. The majority must be processed as an emulsion.
  • Polyol or the isocyanate and the additives is extremely unfavorable. That is, the amounts of additive are very small compared to the amounts of polyol or isocyanate. In an online process, as it is the state of the art, this leads in principle to mixing problems. That's why so far disproportionately large or expensive mixers or mixing systems required. This problem applies equally to PUR and PIR systems.
  • the metering streams of the additives are pulsating due to the small flow rates and the single- or two-cylinder pumps used. This also leads to inhomogeneities in the mixture. In order to obtain continuous, and above all, exact flow rates for the additives, relatively expensive multi-cylinder pumps would have to be used. This problem also applies to both PUR and PIR systems.
  • the thickness of the insulating elements can be very different. It can be 20 mm but also 200 mm. This has the consequence that the Gemischaustragsmengen are variable in a corresponding bandwidth.
  • Another production criterion for insulation elements are recipe changes. That is, a change, e.g. of additives, during ongoing production must be possible.
  • the invention relates to a process for the preparation of insulating elements comprising a layer of polyurethane or polyisocyanurate foam, in which
  • the first reactive component A is mixed with the second reactive component B in at least one mixing head, wherein a reactive mixture is obtained, and
  • step b) the reactive mixture from step b) is discharged from the at least one mixing head and applied to a substrate, on which it reacts out and hardens,
  • step d) the interference of the halogen-free blowing agent in the first reactive component A and / or in the second reactive component B in step a) is carried out such that
  • the reactive component and the halogen-free blowing agent are introduced into the premixer, and the reactive component and the halogen-free blowing agent are mixed in the premixer and discharged as a mixture stream, and separated from the mixture flow of reactive component and halogen-free blowing agent, a partial stream and fed back into the premixer with a homogenizing pump , And the remaining partial flow with at least one metering pump with the metering ⁇ D is conveyed to the at least one mixing head, wherein the
  • Suitable halogen-free blowing agents are e.g. n-pentane, iso-pentane and cyclo-pentane and mixtures of these.
  • Figures 2 and 3 show by way of example the solution for the described task.
  • the described method fulfills all the criteria for an optimized process for the production of insulating elements for thermal insulation.
  • Droplet sizes of about 2 to 80 microns, preferably from about 3 to 50 microns, more preferably from about 4 to 20 microns are achievable in this manner.
  • the delivery flow Vn of the respective homogenization pump is adjustable as a function of the metering flow V D of the at least one corresponding metering pump.
  • the maximum delivery flow Fmax of the respective homogenization pump must be designed for the maximum metering flow Fdmax of the corresponding metering system.
  • the dosing flows of the metering systems are varied by a factor of 10 for a bandwidth of the insulating element thickness of 20 mm to 200 mm, the number of revolutions would then increase by a factor of 10 if the metering currents were minimal, if the respective homogenizing pump were a constant pump.
  • This would heat up the emulsion of the propellant, preferably pentane, and polyol or isocyanate and possibly additives enormously. The resulting heat energy would then have to be dissipated again.
  • gaseous blowing agent components could thereby be formed, which would then be much more difficult to emulsify due to the high volume fraction of the gaseous blowing agent.
  • the essential step of this invention is thus that the flow rate V H of the respective homogenization pump is adapted to the dosing flow V D of the corresponding dosing system. In this way, an optimal operation for the process is possible:
  • the optimal operating point i. the optimum number of revolutions must be determined empirically. It is recognizable by a uniform, fine cell structure of the PUR or PIR foam.
  • the aim is cells of about 0.1 mm in diameter, because the smaller the cell is, the greater the insulating effect.
  • halogen-free blowing agent for example pentane
  • the additives may optionally be blended into either the polyol or the isocyanate component. It is particularly efficient when the interference of halogen-free blowing agent and Additives proportionally carried out both in the polyol and in the isocyanate component. This makes it possible, even higher propellant amounts of pentane than 16 parts by weight, namely up to 25 parts by weight and also beyond, in each case based on the polyol component to interfere in the entire raw material system.
  • the novel process meets all operating requirements if the reactive component A or B is circulated in the respective homogenization cycle one to twenty times, preferably two to ten times, particularly preferably two to five times.
  • the delivery flow Vw of the respective homogenization pump is adjusted by means of a control unit as a function of the corresponding metering flow V D.
  • the control can satisfy a function that is linearly proportional:
  • VH A - VD
  • the system can e.g. To adapt to mixer specific conditions, because if a mixer is designed for a maximum amount, it has a lower efficiency at lower levels, so that the number of passes must be increased disproportionately.
  • the factor A can be chosen in the order of 1 to 20. It is preferably in a range between 1.5 and 10 and more preferably in a range between 2 and 5.
  • the exponent B can be: 0.5 ⁇ B ⁇ 1.5.
  • the quality of the insulating foam correlates with the temperature of the emulsion flowing out of the respective homogenization circuit in cooperation with the adjustment of the delivery flow V H as a function of the corresponding metering flow F D.
  • This provides the possibility of subsequent control of the flow rate fi H of the respective homogenization pump as a function of the corresponding metering flow V D , in which the temperature of the emulsion flowing out of the homogenization cycle is used as the controlled variable.
  • control process and the control process are completely separated from each other and never at the same time.
  • the adjustment of the delivery flow P H of the respective homogenization pump by the controller takes place as a function of the corresponding metering flow P D. Subsequently, the control is switched off and the control of P H in the absence of O takes over. Likewise, the control is turned off when a control operation is again performed.
  • the invention also relates to an apparatus for the production of insulating elements for thermal insulation comprising a layer of polyurethane or polyisocyanurate foam, comprising:
  • At least one mixing head for mixing the reactive components A and B, and for discharging the reactive mixture onto a substrate
  • a pre-mixer circuit upstream charge pump for the promotion of the reactive component A or the reactive component B in the circulation and pressure generation and a biasing valve, through which a partial flow of the funded through the charge pump in the circulation reactive component A or reactive component B is discharged,
  • New in this device is that parallel to the respective premixer or mixing system for the halogen-free blowing agent and optionally for the additives and the corresponding polyol or isocyanate a Homogenmaschinesniklauf is arranged with an adjustable homogenization and this adjustable homogenization each with a control unit with impulse lines of the at least one corresponding metering unit (metering pump) is assigned to the control unit and from the control unit to the adjustable homogenization pump.
  • the respective control unit is combined with a control unit and the respective homogenization cycle is followed by a temperature measuring point ⁇ , each of which leads a pulse line to the control part of the combined control-rule unit.
  • the reactive components are also assigned to gassing devices, by means of which, as a rule, nitrogen is dispersed in. This favors the mixing of the reactive component A with the reactive component B.
  • a mixing element for the halogen-free blowing agent for example pentane, as well as for the additives in the polyol or isocyanate component static mixer, stirrer mixers, rotor-stator mixers or combinations of such mixers can be used.
  • the uniform pre-distribution of the components to be mixed or emulsified takes place by shearing the pentane being divided into droplets.
  • these drops of pentane and additives are then elongated so that they thereby disintegrate into microdroplets of 2 to 80 .mu.m, preferably from 3 to 50 .mu.m, particularly preferably from 4 to 20 .mu.m, so that then a completely homogeneous and especially stable emulsion is formed.
  • the invention also relates to the use of the insulating elements for thermal insulation produced by the process according to the invention.
  • FIG. 1 shows schematically a device for the production of insulating panels according to the prior art.
  • Figure 2 schematically shows an inventive device for the production of insulation boards, in which the halogen-free blowing agent pentane and the additives are mixed into the polyol and the flow of the homogenization pump is adjusted by means of a control unit.
  • Figure 3 schematically a device according to the invention, in which the halogen-free propellant pentane and the additives are also mixed in the polyol and the flow of the homogenization pump is also controlled.
  • Figure 1 shows schematically a device 1 for the production of insulating elements 2 for the
  • a lower cover layer 3 and an upper cover layer 4 are continuously by corresponding feeders 5, 6 in the in Longitudinally extended gap between the circulating upper belt 8 and the circulating lower belt 7 of a so-called Contimaten 1 promoted.
  • the reactive component A (polyol) and the reactive component B (isocyanate) are conveyed via associated suction and pressure lines through the metering pumps 9, 10 to the mixing head 11, where mixed and applied the resulting PIR reaction mixture on the lower cover layer 3.
  • the applied to the lower cover layer 3 PER reaction mixture begins to foam and is transported by the longitudinal movement of the lower cover layer 3 in the forming section, which is formed by the circulating upper belt 8 and the circulating lower belt 7.
  • the PIR reaction mixture foams up between the upper cover layer 4 and the lower cover layer 3 and reacts, so that after passing through the molding section, an endless insulation board is formed, from which individual insulation elements 2 are separated by means of the cutting device 12.
  • the reactive component B contains only isocyanate, which passes from the associated tank 13 to a metering pump 10, the reactive component A polyester polyol, pentane and PER foams specific additives. Pentane and additives are conveyed from associated containers (not shown in the diagram) via associated metering units 14, 15a, 15b, 15c and lines to the stirred premixer 16 where they are mixed into the polyester polyol.
  • the exact dosage of the polyester polyol is carried out by the metering pump 9 for the reactive mixture A, which doses the total amount of polyester polyol, pentane and additives.
  • the polyester polyol recirculates by means of the charge pump 17 from the associated tank 18 via the biasing valve 19, through which the required for the metering pump 9 form is established.
  • the flow rate of the charge pump 17 must be greater than the proportion of polyester polyol removed by the metering pump 9 and the pressure built up by the biasing valve 19 must be higher than the sum of all pressure losses that occur over the entire suction line between the recirculation of the charge pump 17 and the Suction side of the metering pump 9 result.
  • Reactive mixture A through the heat exchanger 21 to the required operating temperature of approx. 18 0 C brought to 20 0 C, before the metering by the metering pump 9 and the mixing with the reactive component B in the mixing head 1 1 takes place.
  • Figure 2 shows schematically a special embodiment of the device according to the invention.
  • insulating elements for thermal insulation are produced by means of a contimates.
  • the Contimat 1 is shown in side view
  • the Contimat 30 is shown with a view to the front, i. the transport direction for the produced insulating elements is perpendicular to the image plane, and indeed in this.
  • FIG. 2 also shows three stationary mixing heads 31, 32, 33, which apply PIR reaction mixture to the lower cover layer resting on the lower belt 34 (not shown in the diagram).
  • Three dosing pumps 35, 36, 37 for the reactive mixture A and three dosing pumps for the reactive component B are assigned to each of these three mixing heads. Furthermore, in each case a heat exchanger is arranged in the pressure lines of these metering pumps 35, 36, 37 to the associated mixing head 31, 32, 33 to set the required PIR process temperature of about 20 0 C to 22 0 C.
  • the metering pumps 35, 36, 37 of the reactive component B are supplied by the associated tank 38 via corresponding suction lines.
  • the reactive mixture A consists in this example of polyester polyol, pentane and PIR foam specific additives, pentane and additives of associated containers and dosing (not shown in the diagram) via an injection block 39 to a special static mixer system comprising static mixers 49A, 49B and 49C promoted and mixed there into the polyester polyol.
  • the exact dosage of the polyester polyol via the associated metering pumps 35, 36, 37 for the reactive mixture A, again an associated tank 40 and a charge pump 41 and a biasing valve 42 ensure the necessary supply of throughput and to form with reactive component A.
  • the novelty in this device according to the invention consists in the fact that parallel to the Einmischumble, ie in this example the static mixer system, for the pentane and the Additive a homogenization circuit with an adjustable homogenization pump 45 is arranged and this adjustable homogenization pump 45 is assigned a control unit 46, to which impulse lines from the adjustable metering pumps 35, 36, 37 of the reactive mixture A and a pulse line lead to the adjustable homogenization pump 45. In this way, it is possible to adjust the flow rate Vn of the homogenizing pump 45 as a function of the metering flow V D removed by the metering pumps 35, 36, 37.
  • the reactive mixture A is circulated through the static mixer system only as often in the homogenization cycle as is necessary in order to produce a perfect, ie homogeneous and stable polyester-pentane additive emulsion. Otherwise, namely, at low flow rates removed from the metering pumps 35, 36, 37, the reactive mixture A would be circulated too frequently, thereby unnecessarily wasting much pump energy and, in addition, introducing too much heat energy into the system, which would subsequently have to be dissipated costly again.
  • V D Working the metering pumps 35, 36, 37 in the upper region, ie V D is about 70% to 100% of the maximum amount, so valve 47 and valve 48 are opened and the corresponding maximum flow Vn of the homogenization pump 45 flows essentially through the large static mixer ie via static mixer 49A.
  • valve 47 is closed as shown in the example, while valve 48 remains open.
  • the corresponding, i. the average flow Vn of the homogenizing pump 45 is first passed through the large static mixer, i. via static mixer 49A, and then substantially via the middle static mixer, i. via static mixer 49B.
  • V D is about 10% to 35% of the maximum quantity
  • This special arrangement of the static mixer has the advantage that not only over the entire volume range optimal mixing is ensured, but that always all three Static mixers are flushed through and no nests with too old material form, which would be the case if the three static mixer and the associated valves would be just arranged in parallel.
  • FIG. 3 shows schematically a further embodiment variant of the device according to the invention. Also in this example, insulating elements for thermal insulation (not shown in the diagram) are produced by means of a Contimaten 60.
  • the metering pump 64 of the reactive component B is supplied from the tank 67 via the suction line.
  • the reactive mixture A consists in these embodiments of polyester polyol, pentane and PIR foam specific additives, pentane and additives of associated containers and dosing (not shown in the diagram) are conveyed via an injection block 68 to a stirred premixer 69 and mixed there.
  • a gas loading device 73 for the Eindispergleiter of nitrogen and a heat exchanger 74 are arranged in the suction line between recirculation of the charge pump 71 and the suction side of the metering pump 63.
  • a gas loading device 73 for the Eindispergleiter of nitrogen and a heat exchanger 74 are arranged in the suction line between recirculation of the charge pump 71 and the suction side of the metering pump 63.
  • a gas loading device 73 for the Eindispergleiter of nitrogen and a heat exchanger 74 are arranged in the suction line between recirculation of the charge pump 71 and the suction side of the metering pump 63.
  • a homogenization circuit with adjustable homogenizing pump 75 is arranged parallel to the injection block 68 and the stirred pre-mixer 69 for the pentane and the additives in the polyester polyol.
  • the novelty in this embodiment with respect to the example shown in Figure 2 is that the adjustable homogenization pump 75 is associated with a combination of a control and a control unit 76.
  • the control component is that in turn by means of pulse lines from the metering pump 63 to the control unit 76 and from the control unit 76 to the homogenizing 76 the flow rate V H of the homogenization pump 75 in response to the dosing flow V D of the metering pump 63 is adjusted.
  • the control component consists in the fact that a further impulse line leads from a homogenizing circuit downstream of the homogenization cycle to the combined control and regulating unit 76, so that the flow Vn of the homogenizing pump 75 is adjusted not only as a function of the metering flow V D but virtually as Fine adjustment depending on ⁇ is also regulated.
  • the control process and the control process are completely separated from each other and never at the same time.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Polyurethanes Or Polyureas (AREA)
  • Casting Or Compression Moulding Of Plastics Or The Like (AREA)

Abstract

L'invention concerne un procédé et un dispositif pour produire des éléments isolants en mousse de polyuréthanne (PUR) ou de polyisocyanurate (PIR). Selon l'invention, l'agent d'expansion est incorporé à au moins un des deux composants réactifs dans un circuit de circulation.
PCT/EP2008/002144 2007-03-28 2008-03-18 Procédé et dispositif pour la production d'éléments isolants Ceased WO2008116575A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007014768.8 2007-03-28
DE102007014768.8A DE102007014768B4 (de) 2007-03-28 2007-03-28 Verfahren und Vorrichtung zur Herstellung von Dämmelementen

Publications (1)

Publication Number Publication Date
WO2008116575A1 true WO2008116575A1 (fr) 2008-10-02

Family

ID=39591762

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/002144 Ceased WO2008116575A1 (fr) 2007-03-28 2008-03-18 Procédé et dispositif pour la production d'éléments isolants

Country Status (2)

Country Link
DE (1) DE102007014768B4 (fr)
WO (1) WO2008116575A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105542646A (zh) * 2015-12-23 2016-05-04 厦门市万旗科技股份有限公司 一种阀门密封用纳米碳酸钙改性复合材料及其制备方法
CN116176008A (zh) * 2023-04-25 2023-05-30 北京维盛复合材料有限公司 一种原材料工艺流量控制系统

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10046487B2 (en) 2011-06-08 2018-08-14 Rim Polymers Industries Pte., Ltd. Methods and apparatus for mixing chemical components for the manufacture of polyurethane
CN119348193B (zh) * 2024-11-19 2025-10-17 中机精密成形产业技术研究院（安徽）股份有限公司 一种双组份hp-rtm设备及搭建方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0368270A1 (fr) * 1988-11-11 1990-05-16 Klöckner Ferromatik Desma GmbH Procédé pour mélanger du polyol et des additifs et dispositif de mise en oeuvre du procédé
US5801210A (en) * 1997-10-29 1998-09-01 Bayer Corporation Method and apparatus for the production of essentially void free foams
WO2003064236A1 (fr) * 2002-01-31 2003-08-07 Hennecke Gmbh Procede pour la production de mousse polyurethanne a structure cellulaire ajustable
US20070291582A1 (en) * 2006-06-02 2007-12-20 Schmidt & Heinzmann Gmbh & Co. Kg Apparatus and method for producing a component mixture from at least two components

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3030106B2 (ja) * 1991-02-22 2000-04-10 三洋電機株式会社 低沸点発泡剤のミキシング装置
DE4235970C1 (de) * 1992-10-26 1993-11-25 Bayer Ag Vorrichtung zum Herstellen eines Schaumstoff bildenden Reaktionsgemisches

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0368270A1 (fr) * 1988-11-11 1990-05-16 Klöckner Ferromatik Desma GmbH Procédé pour mélanger du polyol et des additifs et dispositif de mise en oeuvre du procédé
US5801210A (en) * 1997-10-29 1998-09-01 Bayer Corporation Method and apparatus for the production of essentially void free foams
WO2003064236A1 (fr) * 2002-01-31 2003-08-07 Hennecke Gmbh Procede pour la production de mousse polyurethanne a structure cellulaire ajustable
US20070291582A1 (en) * 2006-06-02 2007-12-20 Schmidt & Heinzmann Gmbh & Co. Kg Apparatus and method for producing a component mixture from at least two components

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105542646A (zh) * 2015-12-23 2016-05-04 厦门市万旗科技股份有限公司 一种阀门密封用纳米碳酸钙改性复合材料及其制备方法
CN116176008A (zh) * 2023-04-25 2023-05-30 北京维盛复合材料有限公司 一种原材料工艺流量控制系统
CN116176008B (zh) * 2023-04-25 2023-08-22 北京维盛复合材料有限公司 一种原材料工艺流量控制系统

Also Published As

Publication number Publication date
DE102007014768A1 (de) 2008-10-02
DE102007014768B4 (de) 2016-09-01

Similar Documents

Publication Publication Date Title
DE69505999T2 (de) Verfahren und vorrichtung zur herstellung von geschlossen-zelligen schaumprodukten
DE69403170T2 (de) Schlagverfahren und System zur kontinuierlichen Herstellung von Polyurethanschaumstoffblocken
DE69610885T2 (de) Verfahren und Gerät zur Herstellung von Polyurethanschaumstoff und Mehrschichtschaumstoffprodukten
DE69523070T2 (de) Extrudierter polymerschaum mit füllstoffteilchen und verfahren
EP0001581B1 (fr) Procédé et dispositif pour mélanger et appliquer des réactifs
EP1539453B1 (fr) Procede de production de mousse polyurethane exempte de poches et de trous d'epingle
DE69614696T2 (de) Verfahren und vorrichtung zum herstellen von kunststoffschaum
WO1997047453A1 (fr) Procede pour la production de mousse a l'aide de dioxyde de carbone dissous sous pression
EP0006519B1 (fr) Procédé et appareil pour préparer un mélange moussant à partir d'au moins deux composants réactifs coulables, formant une mousse, et de charges
DE102007014768B4 (de) Verfahren und Vorrichtung zur Herstellung von Dämmelementen
EP0985444A1 (fr) Procédé et dispositif pour mélanger des produits
DE2339530A1 (de) Misch- und emulgiervorrichtung
EP3281767A1 (fr) Procede et dispositif de fabrication d'une feuille pour dispositif de stockage d'energie electrique
EP0960008B1 (fr) Procede et dispositif permettant de produire du polyurethanne contenant des matieres de remplissage
DE3610159C2 (fr)
EP0183745B1 (fr) Procede et installation de raffinage en continu de matieres a laminer en tant que produit de depart pour le chocolat
EP0566830A1 (fr) Procédé et installation pour la préparation d'une matière à mouler composite fibre/résine, en particulier d'un préimprégné
DE69812888T2 (de) Vorrichtung und verfahren zum herstellen von polymerschaum
EP1846212B1 (fr) Procede et dispositif pour produire une plaque de mousse en polyurethane
EP0615830B1 (fr) Dosage d'un agent moussant pour l'obtention de matières plastiques alvéolaires
DE10203701C1 (de) Verfahren zur Herstellung von Polyurethan-Schaum mit einstellbarer Zellstruktur
DE60121409T2 (de) Verfahren und Vorrichtung zum kontinuierlichen Herstellen von Schaumstoff zur Formung von Paneelen
WO1998039152A1 (fr) Dispositif d'extrusion
EP1487630B8 (fr) Procede de fabrication de semi-produits thermodurcissables
DE60120993T2 (de) Verfahren und apparat zur herstellung von phenolschäume durch vermischung der komponente in einer prallströmung

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: 08716602

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 08716602

Country of ref document: EP

Kind code of ref document: A1