CN102504394A - Production method of filled masterbatch formed through plasticization - Google Patents
Production method of filled masterbatch formed through plasticization Download PDFInfo
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- CN102504394A CN102504394A CN2011103624037A CN201110362403A CN102504394A CN 102504394 A CN102504394 A CN 102504394A CN 2011103624037 A CN2011103624037 A CN 2011103624037A CN 201110362403 A CN201110362403 A CN 201110362403A CN 102504394 A CN102504394 A CN 102504394A
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- 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
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
- B29C48/04—Particle-shaped
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- 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
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- 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
- B29C48/92—Measuring, controlling or regulating
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92504—Controlled parameter
- B29C2948/92704—Temperature
-
- 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
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92819—Location or phase of control
- B29C2948/92857—Extrusion unit
- B29C2948/92876—Feeding, melting, plasticising or pumping zones, e.g. the melt itself
- B29C2948/92895—Barrel or housing
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
Abstract
The invention relates to a production method of a filled masterbatch formed through plasticization. The filled masterbatch is composed of the following components in parts by weight: 5 to 16 parts of carrier resin, 3 to 8 parts of dispersant, 75 to 90 parts of inorganic filler, and 0.5 to 2 parts of surface-active agent. The production method comprises the following steps: stirring and mixing carrier resin and dispersants at a high speed, extruding and granulating the mixture of the carrier resin and dispersants by a co-rotating twin screw extrusion machine, and considering the mixture of the carrier resin and the dispersants as a standby material; stirring and mixing inorganic fillers, the surface-active agent and the standby material at a high speed, discharging and breaking the mixture of the inorganic fillers, the surface-active agent and the standby material, extruding and granulating the mixture of the inorganic fillers, the surface-active agent and the standby material by a co-rotating twin screw extrusion machine with the slenderness ratio: 32 to 48, cooling, and screening, finally obtaining the filled masterbatch. The packed masterbatch made through the production method is good in plasticization, the dispersion effect of the inorganic fillers is good, the whiteness is high, the requirement to the equipment is low, the energy consumption is low, and the yield is high.
Description
Technical field
The invention belongs to the master batch manufacturing technology field that inorganic powder combines with macromolecular material, be specifically related to a kind of working method of plasticizing forming filler parent granule.
Background technology
The application of filling master batch in plastics can reduce the material cost of plastics; Practice thrift synthetic resins; Also have characteristics such as the plastics of improvement physicals, raising working (machining) efficiency; Having formed in the whole nation and to strengthen masterbatch with filling-modified, blend and take product as the leading factor, with important emerging industry colonies of relevant bonded such as inorganic mineral filler, raw and auxiliary material, processing aid and special machinery manufacturings, also is one of industry active, the most with fastest developing speed in the present plastic working industry.
Filler parent granule is a kind of more unmanageable material, and for reaching plasticizing fully, the mineral filler good dispersivity is to the very high requirement of the mixing proposition of the plasticizing of molding device.At present, producing filler parent granule conventional process method is after earlier mineral filler being added the high mixer surface active, again with dispersion agent, processing aid and vector resin pre-mixing, at last through the dual-screw pelletizer extruding pelletization.For example, the Chinese patent publication number is that CN101429686A discloses the good polymer master batch of a kind of dispersing property, and the concrete steps of its preparation are:
(1) the inorganic mineral powder finishing is handled: take by weighing inorganic mineral powder, place high-speed mixer, start and stir, elevated temperature to 110 ℃ was kept 10 minutes, removed moisture; Add coating materials then, stirred 10 ~ 20 minutes; The test degree of activation reaches 100%, gets final product;
(2) the pre-dispersed processing of inorganic mineral powder: the inorganic mineral powder after step (1) finishing is placed kneader, add dispersion agent, be heated to 110 ~ 130 ℃, carry out pre-dispersed processing, 10 minutes time, the back cooling is pulverized;
(3) mixing, granulation: said pre-dispersed back inorganic mineral powder is placed high-speed mixer, adds vector resin, start and stir, mixed 10 minutes, then, feed twin screw extruder, plastify, mixing, extrude, granulation; The processing condition of said twin screw extruder are: 160 ~ 196 ℃ of temperature, 200 ~ 500 rev/mins of screw speeds.
In this technology; The plasticizing of vector resin and the mixing effect of plasticizing that the coating of mineral filler is mainly relied on tablets press; Tablets press is required height, all need bigger screw rod of length-to-diameter ratio and stronger screw combinations usually, just can produce and plastify filler parent granule complete, good dispersivity.Therefore, this process method is high to equipment requirements, energy consumption big, yield poorly, and the mixing effect of high-intensity plasticizing causes material degraded, variable color easily, influences the quality of filler parent granule.
Summary of the invention
The objective of the invention is the deficiency to the aforesaid method proposition, a kind of working method of plasticizing forming filler parent granule is provided, the filler parent granule that this method makes plastifies, and the mineral filler dispersion effect is good, and whiteness is high, and low for equipment requirements, and energy consumption is little, and output is high.
The present invention realizes through following technical scheme:
A kind of working method of plasticizing forming filler parent granule, its raw material consumption is counted by weight:
5 ~ 20 parts of vector resins
3 ~ 8 parts of dispersion agents
75 ~ 120 parts of mineral fillers
0.5 ~ 2 part of surfactant;
Comprise the steps:
(1) vector resin and dispersion agent are added in the high-speed mixer, stirred 2 minutes, in the compound adding parallel dual-screw extruding machine with gained, at 120 ~ 160 ℃ of following extruding pelletizations, as standby material;
(2) mineral filler is added the high-speed mixer stirring and is heated to 100 ~ 110 ℃; Exhaust adds high-speed mixer with surfactant again, stirs 10 ~ 15 minutes; At last the prepared standby material of step (1) is added in the high-speed mixer and stirred 4 ~ 6 minutes; Discharging, fragmentation promptly obtains compound;
(3) step (2) gained compound being added length-to-diameter ratio is that at 140 ~ 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 32 ~ 48 the parallel dual-screw extruding machine.
The melting index of said vector resin is 2 ~ 7g/10min, and vector resin is one or more the combination in new LDPE (film grade), linear low density polyethylene and the high density polyethylene(HDPE).
Said dispersion agent is one or more the combination in white oil, paraffin, polyethylene wax, OPE, Triple Pressed Stearic Acid and stearic acid compound and the ethylene bis stearamide; Stearic acid compound
Said mineral filler is one or more compounds in lime carbonate, talcum powder, permanent white and the Sodium sulfate anhydrous.min(99); The order number of mineral filler is 600 ~ 3000 orders.
Said surfactant is one or more combinations in Triple Pressed Stearic Acid, silane coupling agent, titanate coupling agent, the aluminate coupling agent; Silane coupling agent is KH-550 or KH-570.
The invention has the beneficial effects as follows:
1, working method of the present invention can improve the plasticizing effect of filler parent granule, the dispersiveness of reinforcing inorganic.
2, existing method of producing master batch requires high to tablets press; Usually all need bigger screw rod of length-to-diameter ratio and stronger screw combinations; Just can produce and plastify filler parent granule complete, good dispersivity, and the present invention is smaller to the wearing and tearing of production unit, can shorten the high-strength shear heat course in the material forming process; Reduce the degraded of material, improve the quality of filler parent granule.
3, raw material has passed through a pre-mixing through preplasticizing among the present invention, so when passing through tablets press again, molding device is required low, does not need the very big screw rod of length-to-diameter ratio, reduces equipment loss, and energy consumption is low, and output is high.
Specific embodiments
Below in conjunction with embodiment the present invention is described in further detail, but embodiment of the present invention is not limited to the scope that embodiment representes.
Embodiment 1:
Get material by weight: lime carbonate 800 order 120kg, new LDPE (film grade) 8kg, linear low density polyethylene 4kg, paraffin 6kg, Triple Pressed Stearic Acid 1kg.
Carry out as follows:
(1) with the 8kg new LDPE (film grade), 4kg linear low density polyethylene, 6kg paraffin add in the high-speed mixer, start and stir, and stir 2 minutes, in the compound adding parallel dual-screw extruding machine with gained, at 140 ℃ of following extruding pelletizations, as standby material;
(2) 120kg lime carbonate is added the high-speed mixer stirring and is heated to 110 ℃, exhaust adds high-speed mixer with the 1kg Triple Pressed Stearic Acid again; Stirred 15 minutes, and the prepared standby material of step (1) was added in the high-speed mixer stirred discharging 4 minutes at last; Fragmentation promptly obtains compound;
(3) step (2) gained compound being added length-to-diameter ratio is that at 160 ℃ of following extruding pelletizations, cooling gets product after the screening in 36 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、165℃、162℃、160℃、158℃、155℃、153℃、150℃、150℃
Screw speed: 320r/min.
Embodiment 2:
Get material by weight: lime carbonate 1250 order 120kg, new LDPE (film grade) 8kg, linear low density polyethylene 5kg, polyethylene wax 6kg, Triple Pressed Stearic Acid 2kg, titanate coupling agent 1kg.
Carry out as follows:
(1). with the 8kg new LDPE (film grade), 5kg linear low density polyethylene, 6kg polyethylene wax; The 2kg Triple Pressed Stearic Acid adds in the high-speed mixer, starts and stirs, and stirs 2 minutes; The compound of gained is added in the parallel dual-screw extruding machine, at 120 ℃ of following extruding pelletizations, as standby material;
(2). 120kg lime carbonate is added the high-speed mixer stirring and is heated to 100 ℃; Exhaust is sprayed into the titanate coupling agent of 1kg then while stirring, and high mixer continues to stir 10 minutes after the been sprayed; Again that step (1) is prepared material for making clothes adds high mixer and stirred discharging 5 minutes;
(3) step (2) gained compound being added length-to-diameter ratio is that at 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 36 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、170℃、170℃、167℃、165℃、162℃、160℃、158℃、155℃
Screw speed: 250r/min
Embodiment 3:
By weight: permanent white 2500 order 120kg, new LDPE (film grade) 12kg, linear low density polyethylene 8kg, polyethylene wax 6kg, Triple Pressed Stearic Acid 2kg, silane coupling agent 2kg.
Carry out as follows:
(1) with the 12kg new LDPE (film grade), 8kg linear low density polyethylene, 6kg polyethylene wax; The 1kg Triple Pressed Stearic Acid adds in the high-speed mixer, starts and stirs, and stirs 2 minutes; The compound of gained is added in the parallel dual-screw extruding machine, at 160 ℃ of following extruding pelletizations, as standby material;
(2) 120kg permanent white is added high-speed mixer and stir and be heated to 100 ℃, exhaust is sprayed into the silane coupling agent of 1kg then while stirring; High mixer continues to stir 12 minutes after the been sprayed, adds the 1kg Triple Pressed Stearic Acid then, stirs 5 minutes; Standby material with step (1) adds high-speed mixer stirring 6 minutes at last; Discharging, fragmentation promptly gets compound;
(3) the gained compound being added length-to-diameter ratio is 36 parallel dual-screw extruding machine extruding pelletizations, at 140 ℃ of following extruding pelletizations, gets product after the cooling screening.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、165℃、170℃、170℃、168℃、168℃、165℃、162℃、160℃
Screw speed: 180r/min.
Embodiment 4:
Get material by weight: Sodium sulfate anhydrous.min(99) 1250 order 120kg, new LDPE (film grade) 6kg, linear low density polyethylene 5kg, polyethylene wax 5kg, Triple Pressed Stearic Acid 1.5kg, silane coupling agent 1kg.
Carry out as follows:
(1). with the 6kg new LDPE (film grade), 5kg linear low density polyethylene, 5kg polyethylene wax; The 2kg Triple Pressed Stearic Acid adds in the high-speed mixer, starts and stirs, and stirs 2 minutes; The compound of gained is added in the parallel dual-screw extruding machine, at 120 ℃ of following extruding pelletizations, as standby material;
(2). the 120kg Sodium sulfate anhydrous.min(99) is added the high-speed mixer stirring and is heated to 100 ℃; Exhaust is sprayed into the silane coupling agent of 1kg then while stirring, and high mixer continues to stir 10 minutes after the been sprayed; Again that step (1) is prepared material for making clothes adds high mixer and stirred discharging 5 minutes;
(3) step (2) gained compound being added length-to-diameter ratio is that at 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 36 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、160℃、160℃、158℃、155℃、153℃、150℃、148℃、145℃
Screw speed: 300r/min.
Embodiment 5:
Get material by weight: Sodium sulfate anhydrous.min(99) 1250 order 90kg, talcum powder 1250 order 30kg, new LDPE (film grade) 4kg, linear low density polyethylene 5kg, polyethylene wax 5kg, Triple Pressed Stearic Acid 2kg, silane coupling agent 1kg.
Carry out as follows:
(1) with the 4kg new LDPE (film grade), 5kg linear low density polyethylene, 5kg polyethylene wax; The 2kg Triple Pressed Stearic Acid adds in the high-speed mixer, starts and stirs, and stirs 2 minutes; The compound of gained is added in the parallel dual-screw extruding machine, at 120 ℃ of following extruding pelletizations, as standby material;
(2) talcum powder with 90kg Sodium sulfate anhydrous.min(99) and 30kg adds the high-speed mixer stirring and is heated to 100 ℃; Exhaust; Be sprayed into the silane coupling agent of 1kg then while stirring; High mixer continues to stir 10 minutes after the been sprayed, and again that step (1) is prepared material for making clothes adds high mixer and stirred discharging 5 minutes;
(3) step (2) gained compound being added length-to-diameter ratio is that at 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 36 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、165℃、165℃、162℃、160℃、158℃、155℃、153℃、150℃
Screw speed: 240r/min.
Embodiment 6:
Get material by weight: lime carbonate 600 order 75kg, high density polyethylene(HDPE) 5kg, white oil 3kg, aluminate coupling agent 0.5kg.
Carry out as follows:
(1) with the 5kg high density polyethylene(HDPE), the 3kg white oil adds in the high-speed mixer, starts and stirs, and stirs 2 minutes, in the compound adding parallel dual-screw extruding machine with gained, at 150 ℃ of following extruding pelletizations, as standby material;
(2) 75kg lime carbonate is added the high-speed mixer stirring and is heated to 105 ℃; Exhaust adds high-speed mixer with the 0.5kg aluminate coupling agent again, stirs 13 minutes; At last the prepared standby material of step (1) is added in the high-speed mixer and stirred 5 minutes; Discharging, fragmentation promptly obtains compound;
(3) step (2) gained compound being added length-to-diameter ratio is that at 150 ℃ of following extruding pelletizations, cooling gets product after the screening in 32 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、165℃、162℃、160℃、158℃、155℃、153℃、150℃、150℃
Screw speed: 180r/min.
Embodiment 7:
Get material by weight: Sodium sulfate anhydrous.min(99) 3000 order 80kg, talcum powder 3000 order 20kg, high density polyethylene(HDPE) 7kg, linear low density polyethylene 7kg, OPE 6kg, Triple Pressed Stearic Acid 1.5kg, KH-550 1kg.
Carry out as follows:
(1) with the 7kg high density polyethylene(HDPE), 7kg linear low density polyethylene, 6kg OPE; 1.5kg Triple Pressed Stearic Acid adds in the high-speed mixer, starts and stirs, and stirs 2 minutes; The compound of gained is added in the parallel dual-screw extruding machine, at 130 ℃ of following extruding pelletizations, as standby material;
(2) 80kg Sodium sulfate anhydrous.min(99) and 20kg talcum powder are added the high-speed mixer stirring and be heated to 100 ℃; Exhaust is sprayed into the KH-550 of 1kg then while stirring, and high mixer continues to stir 12 minutes after the been sprayed; Again that step (1) is prepared material for making clothes adds high mixer and stirred discharging 5 minutes;
(3) step (2) gained compound being added length-to-diameter ratio is that at 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 48 the parallel dual-screw extruding machine.
In the granulation process, parallel dual-screw extruding machine forcing machine processing parameter:
Temperature is set:
150℃、160℃、160℃、158℃、155℃、153℃、150℃、148℃、145℃
Screw speed: 300r/min.
Claims (8)
1. the working method of a plasticizing forming filler parent granule, it is characterized in that: its raw material consumption is counted by weight:
5 ~ 20 parts of vector resins
3 ~ 8 parts of dispersion agents
75 ~ 120 parts of mineral fillers
0.5 ~ 2 part of surfactant;
Comprise the steps:
(1) vector resin and dispersion agent are added in the high-speed mixer, stirred 2 minutes, in the compound adding parallel dual-screw extruding machine with gained, at 120 ~ 160 ℃ of following extruding pelletizations, as standby material;
(2) mineral filler is added the high-speed mixer stirring and is heated to 100 ~ 110 ℃; Exhaust adds high-speed mixer with surfactant again, stirs 10 ~ 15 minutes; At last the prepared standby material of step (1) is added in the high-speed mixer and stirred 4 ~ 6 minutes; Discharging, fragmentation promptly obtains compound;
(3) step (2) gained compound being added length-to-diameter ratio is that at 140 ~ 180 ℃ of following extruding pelletizations, cooling gets product after the screening in 32 ~ 48 the parallel dual-screw extruding machine.
2. the working method of a kind of plasticizing forming filler parent granule according to claim 1 is characterized in that: the melting index of said vector resin is 2 ~ 7g/10min.
3. the working method of a kind of plasticizing forming filler parent granule according to claim 1 and 2 is characterized in that: said vector resin is one or more the combination in new LDPE (film grade), linear low density polyethylene and the high density polyethylene(HDPE).
4. the working method of a kind of plasticizing forming filler parent granule according to claim 1 is characterized in that: said dispersion agent is one or more the combination in white oil, paraffin, polyethylene wax, OPE, Triple Pressed Stearic Acid and stearic acid compound and the ethylene bis stearamide.
5. the working method of a kind of plasticizing forming filler parent granule according to claim 1 is characterized in that: said mineral filler is one or more compounds in lime carbonate, talcum powder, permanent white and the Sodium sulfate anhydrous.min(99).
6. according to the working method of claim 1 or 5 described a kind of plasticizing forming filler parent granules, it is characterized in that: the order number of said mineral filler is 600 ~ 3000 orders.
7. the working method of a kind of plasticizing forming filler parent granule according to claim 1 is characterized in that: said surfactant is one or more combinations in Triple Pressed Stearic Acid, silane coupling agent, titanate coupling agent, the aluminate coupling agent.
8. the working method of a kind of plasticizing forming filler parent granule according to claim 7 is characterized in that: said silane coupling agent is KH-550 or KH-570.
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| CN2011103624037A CN102504394B (en) | 2011-11-16 | 2011-11-16 | Production method of filled masterbatch formed through plasticization |
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| CN2011103624037A CN102504394B (en) | 2011-11-16 | 2011-11-16 | Production method of filled masterbatch formed through plasticization |
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| CN104163967A (en) * | 2013-05-20 | 2014-11-26 | 青岛供八方塑料有限公司 | Filling master-batch, polyethylene modified film with filling master-batch, and production method thereof |
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| CN101429686A (en) * | 2008-12-11 | 2009-05-13 | 吴国铭 | Polymer master batch with good dispersibility and its production method and application |
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| CN102504394B (en) | 2013-10-30 |
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