CN102617946B - Method for improving effective blending of polymers with different viscosities by aid of supercritical fluids - Google Patents
Method for improving effective blending of polymers with different viscosities by aid of supercritical fluids Download PDFInfo
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- 239000012530 fluid Substances 0.000 title claims abstract description 68
- 238000000034 method Methods 0.000 title claims abstract description 45
- 229920000642 polymer Polymers 0.000 title claims abstract description 34
- 238000002156 mixing Methods 0.000 title abstract description 14
- 239000000155 melt Substances 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims description 60
- 239000000126 substance Substances 0.000 claims description 52
- 239000004793 Polystyrene Substances 0.000 claims description 30
- 229920001684 low density polyethylene Polymers 0.000 claims description 30
- 239000004702 low-density polyethylene Substances 0.000 claims description 30
- 229920002223 polystyrene Polymers 0.000 claims description 30
- 238000002347 injection Methods 0.000 claims description 22
- 239000007924 injection Substances 0.000 claims description 22
- 229920002302 Nylon 6,6 Polymers 0.000 claims description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 229920010741 Ultra High Molecular Weight Polyethylene (UHMWPE) Polymers 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 7
- 230000006837 decompression Effects 0.000 claims description 7
- 230000007423 decrease Effects 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 6
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 claims description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 2
- 239000006185 dispersion Substances 0.000 abstract description 5
- 239000011159 matrix material Substances 0.000 abstract description 4
- 230000000704 physical effect Effects 0.000 abstract description 3
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- 229920006158 high molecular weight polymer Polymers 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
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- 229920002959 polymer blend Polymers 0.000 description 3
- 229920001155 polypropylene Polymers 0.000 description 3
- 229920005606 polypropylene copolymer Polymers 0.000 description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000000654 additive Substances 0.000 description 2
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- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
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- 239000004811 fluoropolymer Substances 0.000 description 2
- 229920002313 fluoropolymer Polymers 0.000 description 2
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- 239000002114 nanocomposite Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
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- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical group [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
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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
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/395—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders
- B29C48/40—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders using two or more parallel screws or at least two parallel non-intermeshing screws, e.g. twin screw extruders
Abstract
The invention discloses a method for improving effective blending of polymers with different viscosities by the aid of supercritical fluids. The method includes the steps: filling the supercritical fluids into mixed melts of the polymers with the different viscosities; stirring the mixed melts until the first viscosity of the mixed melts is lower than the initial viscosity of the mixed melts in a molten state; and reducing temperature while continuously stirring until the second viscosity of the mixed melts is slightly increased, and reducing pressure and exhausting air. By the aid of plasticization of the supercritical fluids for the polymers, some physical properties of the polymers are changed, for example, the viscosities are reduced, the free volume is increased, molecular chain mobility is enhanced and the like, and two-phase or multi-phase viscosity ratio and interfacial tension can be reduced, so that split-phase degree is improved, dispersion of dispersed phases in a polymer matrix is improved, and power consumption for processing the polymers with the different viscosities in equipment such as an extruder and the like can be reduced.
Description
Technical field
The present invention relates to polymer processing field, be specifically related to a kind of method that adopts supercutical fluid to improve the effective blend of polymkeric substance that viscosity is different.
Background technology
Polymer blending is the problem of academia and industry member extensive concern, and optimizing blend morphology is one of key factor obtained the high-performance polymer intermingling material.When the polymkeric substance that adopts traditional melt processing method to differ greatly to viscosity difference especially viscosity carries out blend, the component that viscosity is low produces the high shear rate district that is separated and enters mixing equipment usually, and the mixing quality of blend descends with the increase of component differences in viscosity.Traditional solution is in full-bodied polymeric matrix, progressively to add low viscosity component, progressively to reduce the differences in viscosity of two components.But when these two component compatibilities were poor, this method also was difficult to prove effective.
Technology about effective blend method of the different polymkeric substance of viscosity in prior art yet there are no report, and more about the method for polymer blending:
A kind of method of high-molecular weight polymer and low-molecular weight polymer melt blending is disclosed in Chinese patent application CN93117066.4, this high-molecular weight polymer, in predetermined melt blending temperature and shearing rate, be that 100 viscosity under falling second are greater than approximately 50000 pools, this low-molecular weight polymer is that 100 viscosity under falling second are less than approximately 3000 pools in this melt blending temperature and shearing rate, the method comprises: (1) low-molecular weight polymer and high-molecular weight polymer at the first stage melt blending to form initial polymer blend, (2) melt blending in the low-molecular weight polymer supplemented and the subordinate phase of this initial polymer blend after the first stage to form final polymer blend.The method is for the different polymkeric substance of molecular weight.
The aqueous dispersion of the (per) fluoropolymer that the PTFE in Chinese patent ZL200680042926.0, non-melt flowed and melting are molded mixes; then reclaim the granular mixture of the dispersion of these polymkeric substance that obtain; and the granular mixture that melting mixing obtains is to obtain blend; wherein the PTFE particle forms disperse phase and (per) fluoropolymer formation external phase; this melting mixing has produced favourable melt viscosity; even in the PTFE content situation of higher approximately 30WT%, this blend also has good physicals.
A kind of method for preparing polypropylene-blend polymer is disclosed in Chinese patent ZL200580019446.8, it is at least a and described polypropylene and/or inconsistent other polymkeric substance of polypropylene copolymer of 10～30 % by weight that this blend contains polypropylene that the share that accounts for respectively this blend polymer gross weight is 40～80 % by weight and/or polypropylene copolymer and share, wherein, by described polypropylene and/or polypropylene copolymer and described other polymer melted, and described melt is under shear conditions, adding strong fusion under organically-modified nanocomposite filler, described nanocomposite filler is aluminium lamination shape silicate, it carries out modification with at least a organic modifiers and at least a additive, wherein said organic modifiers is selected from ammonium compound, sulfonium compound is with phosphonium compounds, they contain the long-chain carbochain of 12～22 carbon atoms with at least one, described additive is selected from lipid acid and derivative of fatty acid, and the organic constituent of non-negatively charged ion, it contains at least one aliphatic series that contains 6～32 carbon atoms or cyclic group.
Supercutical fluid refers to that temperature and pressure is respectively higher than the dense fluid of stagnation point.The characteristic of supercutical fluid is mainly manifested in the density similar liquids, thereby solvating ability is very strong, and the pressure and temperature subtle change can cause its density noticeable change; The variation of pressure and temperature all can change phase transformation; Viscosity, spread coefficient, close to gas, have and transmit very by force performance and movement velocity.Supercutical fluid has the character of gas and liquid concurrently, and it had both had liquid and solute has been had to the characteristics of larger solubleness, has again gas and is easy to the characteristic that spreads and move, and rate of mass transfer is much higher than liquid phase cracking process.
Summary of the invention
The present invention is directed to the deficiencies in the prior art a kind of method that adopts supercutical fluid to improve the effective blend of polymkeric substance that viscosity is different is provided, can realize the especially effective blend between the polymkeric substance that differs greatly of viscosity of viscosity difference.
A kind of method that adopts supercutical fluid to improve the effective blend of polymkeric substance that viscosity is different comprises step:
In the mixed melt of the different polymkeric substance of viscosity, inject supercutical fluid, under molten state, be stirred to the initial viscosity of the first viscosity of mixed melt lower than mixed melt, then at the situation decline low temperature continue stirred until the second viscosity of mixed melt slightly be improved after decompression exhaust, obtain blend polymer.
The polymkeric substance that described viscosity is different has two kinds of different types of component of polymer at least, in traditional polymer blending mode, because the viscosity ratio of the different polymkeric substance of viscosity has difference, especially the viscosity ratio of the polymkeric substance that differs greatly of viscosity has big difference, the easy layering of melt; And adopt the inventive method can reach viscosity ratio and the interfacial tension that reduces two-phase or multiphase, and improve the degree of phase-splitting, improve the dispersion situation of disperse phase in polymeric matrix.In the different polymkeric substance of described viscosity, the ratio of each polymkeric substance does not have strict restriction, arbitrarily than all can, one removes and can configure according to each polymer raw material proportioning of blend polymer to be prepared the consumption of each polymkeric substance.
Melt flow rate (MFR) difference between the polymkeric substance that described viscosity is different is mutual is at least 20g/10min, being preferably polymkeric substance that viscosity the is different melt flow rate (MFR) difference between mutually and being at least 35g/10min, is mainly more can highlight the unusual effect of the inventive method while due to viscosity, differing larger.For example, the polymkeric substance that described viscosity is different can be polystyrene and Low Density Polyethylene, or is ultrahigh molecular weight polyethylene(UHMWPE) and nylon 66 (being polyamide 66).
Described supercutical fluid is selected to have lower than the supercritical temperature of 400 degrees centigrade with lower than the pure gas of 500 handkerchief supercritical pressures or have lower than the supercritical temperature of 400 degrees centigrade with lower than the mixed gas of 500 handkerchief supercritical pressures, as one or more the mixture in supercritical carbon dioxide fluid, overcritical nitrogen fluid, supercritical propane fluid, supercritical methane fluid, overcritical ethane fluid, overcritical trifluoromethane fluid.When the polymkeric substance that described viscosity is different is polystyrene and Low Density Polyethylene, described supercutical fluid is preferably supercritical carbon dioxide fluid, when the polymkeric substance that perhaps described viscosity is different was ultrahigh molecular weight polyethylene(UHMWPE) and nylon 66, described supercutical fluid was preferably overcritical ethane fluid.
In order to reach better effect, preferably: the first viscosity that is stirred to mixed melt under molten state meets following relational expression:
The initial viscosity of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt * 100% >=20%.
Then at the situation decline low temperature continue stirred until the initial viscosity of the second viscosity of mixed melt and mixed melt maintains an equal level or until the second viscosity of mixed melt than the initial viscosity height of mixed melt after decompression exhaust.
The inventive method can realize in the common equipment of this area, as twin screw extruder etc., the equipment of employing such as the parameter of twin screw extruder arrange according to the performance of polymer raw material in blend polymer to be prepared.Due to the swelling action of supercutical fluid to polymkeric substance, the viscosity of mixed melt starts to be what the increase with the supercutical fluid injection rate increased, but when join a certain amount of after, supercutical fluid weakens the swelling action of polymkeric substance, thereby after this, the increase of supercutical fluid injection rate is little on the impact of mixed melt viscosity.The injection rate of the supercutical fluid in general production process described in the production process that adopts twin screw extruder can be controlled by injection speed, the present invention finds that the injection speed of supercutical fluid, the injection speed of mixed melt have larger impact from the blend effect of comparing the polymkeric substance that viscosity is different of the injection speed of supercutical fluid in addition, the injection speed of preferred supercritical fluid is 2g/min～6g/min, and the injection speed of mixed melt is 250～350: 1 with the ratio of the injection speed of supercutical fluid.
Compared with prior art, the present invention has following advantage:
The characteristics of the inventive method are that supercutical fluid is injected in the mixed melt of the polymkeric substance that viscosity is different (polymkeric substance differed greatly as viscosity), utilize the plastification of supercutical fluid to polymkeric substance, some physical properties of polymkeric substance is changed, as reduced viscosity, free volume increases, molecular chain mobility enhancing etc., can reduce two-phase or multiphase viscosity ratio and interfacial tension, thereby improve the degree of phase-splitting, improve the dispersion situation of disperse phase in polymeric matrix, also help simultaneously to reduce the polymkeric substance that viscosity is different and in the equipment such as forcing machine, add the power consumption in man-hour.
The supercutical fluid adopted in the inventive method have the diffustivity of similar gas and liquid density, nontoxic, do not fire, cheap and easy to get, reclaim the characteristics such as simple, easy to use, without reclaiming and aftertreatment, non-wastewater discharge, meet the requirement of Green Chemistry.
The accompanying drawing explanation
Fig. 1 is the electron-microscope scanning figure of nylon 66/ super high molecular weight polyethylene blend in Comparative Examples 2;
Fig. 2 is the electron-microscope scanning figure of nylon 66/ super high molecular weight polyethylene blend in embodiment 2.
Embodiment
Below by embodiment, the present invention is specifically described; be necessary to be pointed out that at this following examples only are used to further illustrate the present invention; can not be interpreted as limiting the scope of the invention, the person skilled in the art in this field can make some nonessential improvement and adjustment to the present invention according to foregoing.
Embodiment 1
Polystyrene (melt flow rate (MFR) is 1.5g/10min) and Low Density Polyethylene (melt flow rate (MFR) is 40g/10min) are that two kinds of viscosity differ larger polymkeric substance.After the Low Density Polyethylene of the polystyrene of 50kg and 50kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 32: 1, the injection speed of mixed with polymers melt is 500g/min.By on the twin screw extruder barrel, adding pore by continuous being injected in the mixed with polymers melt of supercritical carbon dioxide fluid, the injection speed of supercritical carbon dioxide fluid is 2g/min, the control screw speed is: 100 rev/mins, control twin screw and to the temperature of head, be respectively 150 ℃ by feed zone, 170 ℃, 170 ℃, 160 ℃, 155 ℃ of head temperatures, extruding pelletization, this process can guarantee that the first viscosity that is stirred to mixed melt under molten state meets following relational expression: the initial viscosity * 100%=20% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, then continuing the situation decline low temperature stirred until the fair rear decompression exhaust of the initial viscosity of the second viscosity of mixed melt and mixed melt, obtain polystyrene/low density polyethylene blends, the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows that the inventive method has obtained polystyrene and the Low Density Polyethylene uniform blend that all distributes.
In whole operating process, the electric current of the motor of twin screw extruder is 90 amperes, obviously reduces than 135 amperes in Comparative Examples 1, has greatly saved the energy consumption in the production process.
Comparative Examples 1
Polystyrene (melt flow rate (MFR) is 1.5g/10min) and Low Density Polyethylene (melt flow rate (MFR) is 40g/10min) are that two kinds of viscosity differ larger polymkeric substance.After the Low Density Polyethylene of the polystyrene of 50kg and 50kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 32: 1, the injection speed of mixed with polymers melt is 500g/min.The control screw speed is: 100 rev/mins, control twin screw and to the temperature of head, be respectively 150 ℃, 170 ℃, 170 ℃, 160 ℃ by feed zone, 155 ℃ of head temperatures, extruding pelletization, obtain polystyrene/low density polyethylene blends, in the blend that the effect that the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows does not have supercutical fluid obtains, polystyrene and Low Density Polyethylene all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 135 amperes, and power consumption is larger.
Comparative Examples 2
Except the first viscosity of mixed melt meets following relational expression: the initial viscosity * 100%=10% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, all the other operations are with embodiment 1, obtain polystyrene/low density polyethylene blends, the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows in the blend that the amplitude of the first reduced viscosity of mixed melt hour obtains that polystyrene and Low Density Polyethylene all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 132 amperes, and power consumption is larger.
Embodiment 2
Ultrahigh molecular weight polyethylene(UHMWPE) (melt flow rate (MFR) is near 0g/10min) and nylon 66 (melt flow rate (MFR) is 20g/10min) are that two kinds of viscosity differ larger polymkeric substance, after the ultrahigh molecular weight polyethylene(UHMWPE) of the ultrahigh molecular weight polyethylene(UHMWPE) of 30kg and 70kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 48: 1, the injection speed of mixed with polymers melt is 2000g/min.By on the twin screw extruder barrel, adding pore by continuous being injected in the mixed with polymers melt of overcritical ethane fluid, the injection speed of overcritical ethane fluid is 6g/min, the control screw speed is: 300 rev/mins, control twin screw and to the temperature of head, be respectively 200 ℃ by feed zone, 235 ℃, 235 ℃, 215 ℃, 205 ℃ of head temperatures, extruding pelletization, this process can guarantee that the first viscosity that is stirred to mixed melt under molten state meets following relational expression: the initial viscosity * 100%=60% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, then at the situation decline low temperature continue stirred until the second viscosity of mixed melt than the initial viscosity height of mixed melt after decompression exhaust, obtain nylon 66/ super high molecular weight polyethylene blend, electron-microscope scanning figure such as Fig. 2 of this poly-nylon 66/ super high molecular weight polyethylene blend, in the blend that demonstration the inventive method obtains, nylon 66 and ultrahigh molecular weight polyethylene(UHMWPE) all distribute evenly.
In whole operating process, the electric current of the motor of twin screw extruder is 120 amperes, obviously reduces than 150 amperes in Comparative Examples 2, has greatly saved the energy consumption in the production process.
Comparative Examples 3
Ultrahigh molecular weight polyethylene(UHMWPE) (melt flow rate (MFR) is near 0g/10min) and nylon 66 (melt flow rate (MFR) is 20g/10min) are that two kinds of viscosity differ larger polymkeric substance, after the ultrahigh molecular weight polyethylene(UHMWPE) of the ultrahigh molecular weight polyethylene(UHMWPE) of 30kg and 70kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 48: 1, the injection speed of mixed with polymers melt is 2000g/min.The control screw speed is: 300 rev/mins, control twin screw and to the temperature of head, be respectively 200 ℃, 235 ℃, 235 ℃, 215 ℃ by feed zone, 205 ℃ of head temperatures, extruding pelletization, obtain nylon 66/ super high molecular weight polyethylene blend, should gather electron-microscope scanning figure such as Fig. 1 of nylon 66/ super high molecular weight polyethylene blend, in the blend that the effect that showing does not have supercutical fluid obtains, nylon 66 and ultrahigh molecular weight polyethylene(UHMWPE) all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 150 amperes, and power consumption is larger.
Comparative Examples 4
Except the first viscosity of mixed melt meets following relational expression: the initial viscosity * 100%=15% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, all the other operations are with embodiment 2, obtain nylon 66/ super high molecular weight polyethylene blend, the electron-microscope scanning figure of this poly-nylon 66/ super high molecular weight polyethylene blend shows in the blend that the amplitude of the first reduced viscosity of mixed melt hour obtains that nylon 66 and ultrahigh molecular weight polyethylene(UHMWPE) all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 145 amperes, and power consumption is larger.
Embodiment 3
Polystyrene (melt flow rate (MFR) is 1.5g/10min) and Low Density Polyethylene (melt flow rate (MFR) is 40g/10min) are that two kinds of viscosity differ larger polymkeric substance.After the Low Density Polyethylene of the polystyrene of 60kg and 50kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 32: 1, the injection speed of mixed with polymers melt is 1000g/min.By on the twin screw extruder barrel, adding pore by continuous being injected in the mixed with polymers melt of supercritical carbon dioxide fluid, the injection speed of overcritical nitrogen fluid is 4g/min, the control screw speed is: 200 rev/mins, control twin screw and to the temperature of head, be respectively 150 ℃ by feed zone, 170 ℃, 170 ℃, 160 ℃, 155 ℃ of head temperatures, extruding pelletization, this process can guarantee that the first viscosity that is stirred to mixed melt under molten state meets following relational expression: the initial viscosity * 100%=40% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, then at the situation decline low temperature continue stirred until the second viscosity of mixed melt than the initial viscosity height of mixed melt after decompression exhaust, obtain polystyrene/low density polyethylene blends, the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows that the inventive method has obtained polystyrene and the Low Density Polyethylene uniform blend that all distributes.
In whole operating process, the electric current of the motor of twin screw extruder is 100 amperes, obviously reduces than 142 amperes in Comparative Examples 3, has greatly saved the energy consumption in the production process.
Comparative Examples 5
Polystyrene (melt flow rate (MFR) is 1.5g/10min) and Low Density Polyethylene (melt flow rate (MFR) is 40g/10min) are that two kinds of viscosity differ larger polymkeric substance.After the Low Density Polyethylene of the polystyrene of 60kg and 50kg is uniformly mixed, join intake zone or the loading hopper that length-to-diameter ratio L/D is the twin screw extruder of 32: 1, the injection speed of mixed with polymers melt is 1000g/min.The control screw speed is: 200 rev/mins, control twin screw and to the temperature of head, be respectively 150 ℃, 170 ℃, 170 ℃, 160 ℃ by feed zone, 155 ℃ of head temperatures, extruding pelletization, obtain polystyrene/low density polyethylene blends, in the blend that the effect that the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows does not have supercutical fluid obtains, polystyrene and Low Density Polyethylene all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 142 amperes, and power consumption is larger.
Comparative Examples 6
Except the first viscosity of mixed melt meets following relational expression: the initial viscosity * 100%=19% of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt, all the other operations are with embodiment 2, obtain polystyrene/low density polyethylene blends, the electron-microscope scanning figure of this polystyrene/low density polyethylene blends shows in the blend that the amplitude of the first reduced viscosity of mixed melt hour obtains that polystyrene and Low Density Polyethylene all are uneven distribution.
In whole operating process, the electric current of the motor of twin screw extruder is 145 amperes, and power consumption is larger.
Claims (8)
1. method that adopts supercutical fluid to improve the effective blend of polymkeric substance that viscosity is different comprises step:
In the mixed melt of the different polymkeric substance of viscosity, inject supercutical fluid, under molten state, be stirred to the initial viscosity of the first viscosity of mixed melt lower than mixed melt, then at the situation decline low temperature continue stirred until the second viscosity of mixed melt slightly be improved after decompression exhaust, obtain blend polymer;
The polymkeric substance that described viscosity is different is at least two kinds of different types of polymkeric substance;
The first viscosity that is stirred to mixed melt under molten state meets following relational expression: the initial viscosity of (the first viscosity of the initial viscosity-mixed melt of mixed melt) ÷ mixed melt * 100% >=20%;
Melt flow rate (MFR) difference between the polymkeric substance that described viscosity is different is mutual is at least 20g/10min.
2. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, the melt flow rate (MFR) difference between the polymkeric substance that described viscosity is different is mutual is at least 35g/10min.
3. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, the polymkeric substance that described viscosity is different is polystyrene and Low Density Polyethylene, or is ultrahigh molecular weight polyethylene(UHMWPE) and nylon 66.
4. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, described supercutical fluid is to have lower than the supercritical temperature of 400 degrees centigrade with lower than the pure gas of 500 handkerchief supercritical pressures or have lower than the supercritical temperature of 400 degrees centigrade with lower than the mixed gas of 500 handkerchief supercritical pressures.
5. according to the described employing supercutical fluid of claim 1 or 4, improve the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, described supercutical fluid is one or more the mixture in supercritical carbon dioxide fluid, overcritical nitrogen fluid, supercritical propane fluid, supercritical methane fluid, overcritical ethane fluid, overcritical trifluoromethane fluid.
6. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, the polymkeric substance that described viscosity is different is polystyrene and Low Density Polyethylene, and described supercutical fluid is preferably supercritical carbon dioxide fluid; The polymkeric substance that perhaps described viscosity is different is ultrahigh molecular weight polyethylene(UHMWPE) and nylon 66, and described supercutical fluid is preferably overcritical ethane fluid.
7. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, then at the situation decline low temperature continue stirred until the initial viscosity of the second viscosity of mixed melt and mixed melt maintains an equal level or until the second viscosity of mixed melt than the initial viscosity height of mixed melt after decompression exhaust.
8. employing supercutical fluid according to claim 1 improves the method for the effective blend of polymkeric substance that viscosity is different, it is characterized in that, described method is carried out in twin screw extruder, the injection speed of described supercutical fluid is 2g/min～6g/min, and the injection speed of mixed melt is 250～350:1 with the ratio of the injection speed of supercutical fluid.
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