CN102922618A - Preparation system device and preparation method for high-performance black master-batches - Google Patents

Preparation system device and preparation method for high-performance black master-batches Download PDF

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Publication number
CN102922618A
CN102922618A CN2012103908550A CN201210390855A CN102922618A CN 102922618 A CN102922618 A CN 102922618A CN 2012103908550 A CN2012103908550 A CN 2012103908550A CN 201210390855 A CN201210390855 A CN 201210390855A CN 102922618 A CN102922618 A CN 102922618A
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mixer
carbon black
speed
auxiliary agent
bin
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CN102922618B (en
Inventor
张军
江国栋
陈双俊
杨念新
余新明
杨气鹏
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JIANGSU XINPENG PLASTIFY TECHNOLOGY Co Ltd
Nanjing Tech University
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JIANGSU XINPENG PLASTIFY TECHNOLOGY Co Ltd
Nanjing Tech University
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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
    • 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
    • B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
    • B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
    • B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
    • B29B7/42—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix
    • B29B7/426—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with screw or helix with consecutive casings or screws, e.g. for charging, discharging, 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
    • B29B7/58—Component parts, details or accessories; Auxiliary operations
    • B29B7/60—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material
    • B29B7/603—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material in measured doses, e.g. proportioning of several materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
    • B29B7/58—Component parts, details or accessories; Auxiliary operations
    • B29B7/72—Measuring, controlling or regulating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
    • B29B7/7461—Combinations of dissimilar mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
    • B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
    • B29B7/7485—Systems, i.e. flow charts or diagrams; Plants with consecutive mixers, e.g. with premixing some of the components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/82—Heating or cooling
    • 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
    • B29C48/397—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 a single screw
    • 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
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B9/00—Making granules
    • B29B9/02—Making granules by dividing preformed material
    • B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
    • 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
    • B29C2948/92009—Measured parameter
    • B29C2948/9218—Weight
    • 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
    • B29C2948/92676—Weight
    • 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
    • B29C2948/92828—Raw material handling or dosing, e.g. active hopper or feeding device

Abstract

The invention discloses a preparation system device and a preparation method for high-performance black master-batches. The preparation system device comprises a raw material bin, an integrated feeding system, a dual-rotor continuous mixing mill, a single-screw extruder and a granulator, wherein the integrated feeding system consists of n dynamic weighing systems; each dynamic weighing system consists of a middle bin, a weighing bin and a weight loss scale; the top of the middle bin is connected with the corresponding raw material bin through a sealed conveying pipeline; the middle bin is further connected with a vacuum pump through the sealed pipeline; the bottom of the middle bin is connected with the weighing bin through the sealed pipeline; a switching valve is arranged between the middle bin and the weighing bin; the weighing bin is provided with the weight loss scale for weighing raw materials; the bottom of each weighing bin is connected with the dual-rotor continuous mixing mill through the sealed pipeline; and n is less than or equal to number of used raw materials in the formula. The preparation system device realizes continuous and automatic production, high production efficiency and high stability of product quality.

Description

Preparation system device of a kind of high-performance carbon black masterbatch and preparation method thereof
Technical field
The present invention relates to preparation system device of a kind of master batch and preparation method thereof, more specifically to preparation system device of a kind of high-performance carbon black masterbatch and preparation method thereof.
Background technology
Carbon black is a kind of important functional filler, uses mainly as the reinforcement filler at rubber industry, can be used as ultravioletlight screening agent and black colorant use at plastic industry.Carbon black can be widely used in the aspects such as Plastic Gas pipeline, water purification conveyance conduit, conductive plastics, plastic sheeting and CABLE MATERIALS, as select content more than 2.5%, the ecosystem particle is that the carbon black of 5～20nm is used for plastic products and reaches good dispersion, can effectively shield ultraviolet light to the damage of plastic products, reached more than 50 years its service life.Along with the progress of expanding economy and technology, for the demand phenomenal growth of carbon black, and its application is also constantly expanded in recent years.
Carbon black only has and is dispersed in well in the macromolecular material, its excellent performance of competence exertion, otherwise disperse not good carbon black aggregate not only can not effectively shield ultraviolet light, can become the stress concentration point that macromolecular material destroys at first on the contrary, cause material mechanical performance to descend.Carbon black is difficult to by the process engineering of plastic products it be disperseed equably because apparent density is little, specific area is large.Solving carbon black usually is to adopt special equipment and special formulation at first to prepare black masterbatch in the way of plastic products dispersiveness, and the master batch that contains pre-dispersed carbon black by adding can make carbon black disperse equably in the process engineering of plastic products.The technique of preparation black masterbatch mainly comprises following three kinds at present:
(1) double screw extruder: this technique is that resin, carbon black and function additive etc. are at first mixed through high-speed mixer, then adds double screw extruder blend granulation.The advantage of the method maximum is that equipment is simple, small investment; The shortcoming that exists is that the raw materials such as carbon black and resin easily cause carbon powder dust to fly upward and contaminated environment when mixed at high speed, adopts simultaneously in the black masterbatch of this explained hereafter the carbon black mass degree usually less than 30%.
(2) banbury: this technique is that resin and carbon black are added in the banbury after the weighing respectively by weighing balance, and function additive then is usually by manually putting in the banbury behind the manual weighing; Discharge is to mill after the blend evenly in banbury when resin, carbon black and function additive, and the charge door of sending into single screw extrusion machine by belt conveyor after the mill slice carries out extruding pelletization.The advantage of the method maximum is can produce the carbon black mass degree up to 50% black masterbatch; The shortcoming that exists is that production process is unstable, the content of carbon black fluctuation is large, easily causes loss of material and dust from flying the process from the banbury discharge to mill simultaneously owing to adopt the banbury intermittence to produce.
(3) two-rotor continuous mixer: resin, carbon black and function additive accurately add the two-rotor continuous mixer blend after the weighing simultaneously in containing the dynamic weighting system that a plurality of weight-loss meterings claim, evenly after material utilization deadweight fall into single screw extrusion machine and carry out granulation.The advantage of the method maximum is can produce continuously the carbon black mass degree up to 50% black masterbatch, because production process is continuous, and the black masterbatch steady quality; This process loss of material and dust from flying are all less simultaneously, are the production methods of at present environmental protection.
Available technology adopting double screw extruder, banbury and two-rotor continuous mixer are produced technical process schematic diagram such as Fig. 2, Fig. 3 and shown in Figure 4 of black masterbatch.These three kinds of techniques without exception all be at first to utilize goods with elevator the raw materials such as resin, carbon black to be promoted to the 4th buildings, again by driving a vehicle in the separately feed bin of raw material input between the 3-4 building, enter blending bunker by prescription after the weighing via the material weighing system that is positioned at the 3rd buildings (or the 2nd buildings), entered by blending bunker again and be positioned at 2 building banburies, two-rotor continuous mixer or 1 building double screw extruder and carry out blend and granulation.This system process is long, and it is large to take up room, and equipment and capital construction drop into all larger; Long material resin and the carbon black of also can causing of simultaneously technological process easily flies upward in transportation and production process, causes production environment to pollute and affect workers ' health; In addition technological process length causes the production process energy consumption large, especially adopts banbury and two-rotor continuous mixer technique.
The technique of at present traditional two-rotor continuous mixer production black masterbatch as shown in Figure 4, although this technique is compared the serialization production that has solved black masterbatch with Fig. 3 banbury technique, but material loading and Weighing system more complicated, or the factory building that needs to build up to the 4th buildings carries out the equipment and process layout.In addition, in the traditional elastomeric compound preparation process of rubber industry transformation, brought into use integrated feeding system, can in 1 layer space, the raw material clearance-type be offered banbury, this integrated feeding system takes up room little, equipment investment is also few, capital construction cost and operation costs are low, but through research find this integrated feeding system all be utilize a weighing balance one by one raw materials weighing and various auxiliary agent to the banbury feed, can only gap method explained hereafter, serialization production that can not implementation procedure, and be difficult to carry out accurate weighing and complete conveying for consumption less powder material and auxiliary agent.Such as, require high for the black masterbatch that is used for the special occasions such as Gas Pipe PP Pipe Compound, auxiliary agent is wide in variety and consumption is few in the prescription, thereby auxiliary agent weighing precision prescribed is high, auxiliary agent is easy to produce adhesion in the conveyance conduit of existing integrated feeding system, and is final because the inaccurate poor-performing that causes of composition of raw materials.Therefore, need preparation system device of a kind of high performance black masterbatch of exploitation and preparation method thereof, use with the market that adapts to the black masterbatch expanding day.
Summary of the invention:
The objective of the invention is in order to solve and improve existing black masterbatch poor-performing, the technological process of production is grown, is taken up room greatly, equipment investment is large, production process causes vector resin and carbon black to disperse easily, cause production environment to pollute and affect the problem and shortage of workers ' health, preparation system device of a kind of high-performance carbon black masterbatch and preparation method thereof is provided, the master batch of preparation can be used as ultraviolet light screener and black colorant, is widely used in the aspects such as polyolefin gas pipeline, water purification conveyance conduit, conductive plastics, film and CABLE MATERIALS.
The present invention is achieved by the following technical solutions:
The preparation system device of high-performance carbon black masterbatch provided by the invention; include raw material cabin; integrated feeding system; two-rotor continuous mixer; single screw extrusion machine and pelleter; described integrated feeding system is comprised of n dynamic weighting system; each dynamic weighting system all has intermediate bunker; scale feed bin and Weightlessness balance form; the intermediate bunker top is by sealing conveyance conduit and the connection of corresponding raw material cabin; intermediate bunker also is connected with vavuum pump by closed conduit; the intermediate bunker bottom connects the scale feed bin by closed conduit; be provided with controlled valve between intermediate bunker and the scale feed bin simultaneously; the scale feed bin is equipped with the Weightlessness balance of raw materials weighing; each scale bin bottom is connected with two-rotor continuous mixer by closed conduit again, and wherein n quantity is less than or equal to the quantity of using the raw material number in the prescription.
The preparation system device of high-performance carbon black masterbatch of the present invention, its further technical scheme is that the auxiliary agent feed bin in the described raw material cabin is connected with the high-speed mixer that can first auxiliary agent be diluted by conveyance conduit, described auxiliary agent is diluted is exactly first auxiliary agent and part polyolefin carrier resin to be pre-mixed, mixed material enters the auxiliary agent feed bin, avoided like this adhesion of auxiliary agent in high-speed mixer and conveyance conduit, be conducive to the conveying of auxiliary agent and the stability of course of conveying, simultaneously so that auxiliary agent is prepared and weighing error reduces; Because raw material time of staying in two-rotor continuous mixer is short, utilizes auxiliary agent preparation technique of the present invention and conveying technology, can make that auxiliary agent is easier to be dispersed in the matrix resin quickly and evenly.
The preparation system device of high-performance carbon black masterbatch of the present invention, the control method that its further technical scheme can also be described dynamic weighting system is independent control method or interlock control method, wherein said independent control method is that each weighing subsystem arranges the value of feeding intake by prescription, and independently feeds intake; Described interlock control method is namely set the prescription value of the dynamic weighting system of one of them raw material, the dynamic weighting system of other raw material is according to the actual value of feedback that feeds intake of prescription value of that dynamic weighting system that claims to have set, press formula rate, corresponding adjustment inventory.
The preparation system device that utilizes the high-performance carbon black masterbatch of the present invention prepares the method for high-performance carbon black masterbatch, may further comprise the steps:
Auxiliary agent dilution and mixed at high speed: in high-speed mixer with part polyolefin carrier resin and dispersant in the formula material, processing aid and antioxidant mix, polyolefin carrier resin demand in its high-speed mixer: auxiliary dosage quality proportioning is 5～10: 1, mixed method is that the rotating speed of namely controlling high-speed mixer under the first low-speed conditions stirs 3～8min below 500rpm, then start high-speed stirred and namely control the rotating speed of high-speed mixer more than 1000rpm, get final product discharge behind high-speed stirred 2～5min to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ± 5 ℃ can discharge to the auxiliary agent feed bin;
Integrated material loading and Dynamic Weighting: open integrated feeding system, in intermediate bunker, form vacuum by vavuum pump, the auxiliary agent of the pressure differential of utilizing intermediate bunker and raw material cabin after with carbon black, polyolefin carrier resin, dilution is delivered to the intermediate bunker of dynamic weighting system, various raw materials are continuously directly put into behind the Weightlessness balance automatic gauge in the scale feed bin and are carried out blend in the two-rotor continuous mixer, wherein the two-rotor continuous mixer rotating speed is controlled at 200～550rpm, temperature is at 170～190 ℃, production capacity 200～400kg/h;
The single screw extrusion machine granulation: the material in the two-rotor continuous mixer after the blend is extruded and through the pelleter granulation through single screw extrusion machine again; wherein single screw extrusion machine transportation section temperature is controlled at 70～100 ℃; fluxing zone and head temperature are controlled at 180～220 ℃; screw speed is 40～80rpm, production capacity 200～400kg/h.
Prepared high-performance carbon black masterbatch among preparation system of the present invention and the preparation method, made by the raw material of following quality proportioning:
Figure BSA00000789775200041
High-performance carbon black masterbatch of the present invention, its further technical scheme are that described polyolefin carrier resin is comprised of each raw material with weight portion
High density polyethylene (HDPE) 15-80 part
LLDPE 0-20 part
Ethylene-vinyl acetate copolymer 0-10 part.
The mass content of vinylacetate is 5～15% in therein ethylene-vinyl acetate co-polymer.Middle-high density polyethylene of the present invention is preferably density 0.940-0.963g/cm 3, melt flow rate (MFR) (190 ℃, 2.16kg) one or more pulverulent mixtures of 5～30g/10min; LLDPE is preferably density 0.920-0.935g/cm 3, melt flow rate (MFR) (190 ℃, 2.16kg) one or more pulverulent mixtures of 30-60g/10min; Ethylene-vinyl acetate copolymer is preferably density 0.920-0.940g/cm 3, melt flow rate (MFR) (190 ℃, 2.16kg) one or more particulate mixtures of 5-20g/10min.
High-performance carbon black masterbatch of the present invention, its further technical scheme can also be that described carbon black is to adopt the ecosystem particle of wet processing or dry process production in the kind of 5～20nm low sulfur content.
High-performance carbon black masterbatch of the present invention, its further technical scheme can also be that described dispersant is a kind of in calcium stearate, zinc stearate, the barium stearate or its combination; Described antioxidant is a kind of in phosphite ester kind antioxidant, Hinered phenols antioxidant, the sulphur ester antioxidant or its combination.Further technical scheme is that described phosphorous acid kind antioxidant is tricresyl phosphite (2,4-di-tert-butyl-phenyl) ester or two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites; Described Hinered phenols antioxidant is that four [3-(3,5-di-t-butyl-4-hydroxyphenyl) propionic acid] quaternary amyl alcohol ester, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol), β-(4-hydroxy phenyl-3, the 5-di-t-butyl) the positive octadecanol ester of propionic acid, 2,6-di-tert-butyl-4-methy phenol, 4,4 '-thiobis (the 6-tert-butyl group-3-methylphenol) or 4,4 '-thiobis (6-tert-butyl group metacresol); Described sulphur ester antioxidant is pentaerythrite four (3-lauryl thiopropionate) or β, β '-thio-2 acid distearate.
High-performance carbon black masterbatch of the present invention, its further technical scheme can also be that described processing aid is organic fluoride Dynamar TMPPA.Organic fluoride Dynamar TMPPA (Tai Lema polymer processing aids), that the fluorine high molecular polymer that Dyneon company produces is the additive of foundation structure, has low-surface-energy, can help improve the processing characteristics of polymer, can form in the plastics machinery metal surface " coating " in the plastic processing process, reduce the metal surface adhesion strengths such as melt and machine barrel, screw rod, mouthful mould, improve the inhomogeneous state of bath movement.
Compared with prior art the present invention has following beneficial effect:
The black masterbatch of the present invention preparation, its content of carbon black 20～55%, carbon black dispension degree≤3 grade, moisture content≤0.1%, oxidation induction period (210 ℃) 〉=20min, melt flow rate (MFR) (MFR) (190 ℃, 21.6kg) 〉=20g/10min.Can be used as ultravioletlight screening agent and black colorant, be widely used in the aspects such as polyolefin gas pipeline, water purification conveyance conduit, conductive plastics, film and CABLE MATERIALS.
Integrated feeding system utilizes the pressure differential between intermediate bunker and the independent feed bin in the high-performance carbon black masterbatch preparation system device of the present invention, carry auxiliary agent and raw material by pipeline, many weight-loss meterings claim (more than 4) simultaneously consecutive weighings resin, carbon black and auxiliary agent in the employing dynamic weighting system; This integrated material loading and dynamic weighting system armamentarium and process layout all finish in the 1st building, system have take up room little, equipment investment is few, the capital construction cost and operation costs are low, weighing accurately, can realize the advantage such as serialization production.Also have the following advantages in addition: technological process weak point, raw material negative pressure transportation, closed prescription feed intake, continuous mixing and granulating system, so that raw material are carried in airtight system all the time and are produced, the carbon black leakage can not occur and fly upward phenomenon, guaranteed good production environment; Because serialization and automated production, production efficiency is high, and constant product quality is good.
Utilize in addition auxiliary agent dilution premix of the present invention method preparation and conveying technology, avoided the adhesion of auxiliary agent in high-speed mixer and conveyance conduit, be conducive to the conveying of auxiliary agent and the stability of course of conveying, simultaneously so that auxiliary agent is prepared and weighing error reduces; Because raw material time of staying in continuous birotor mixing roll is short, utilizes auxiliary agent preparation technique of the present invention and conveying technology, can make that auxiliary agent is easier to be dispersed in the matrix resin stability of improving the quality of products quickly and evenly.
Description of drawings
Fig. 1 is high-performance carbon black masterbatch preparation system apparatus structure schematic diagram of the present invention
Fig. 2 is double screw extruder technique black masterbatch production process schematic diagram
Fig. 3 is banbury technique black masterbatch production process schematic diagram
Fig. 4 is two-rotor continuous mixer technique black masterbatch production process schematic diagram
The specific embodiment:
As shown in Figure 1; the preparation system device of employed high-performance carbon black masterbatch is as follows among the embodiment: this device includes raw material cabin; integrated feeding system; two-rotor continuous mixer; single screw extrusion machine and pelleter; described integrated feeding system is comprised of 5 dynamic weighting systems; each dynamic weighting system all has intermediate bunker; scale feed bin and Weightlessness balance form; the intermediate bunker top is by sealing conveyance conduit and the connection of corresponding raw material cabin; intermediate bunker also is connected with vavuum pump by closed conduit; the intermediate bunker bottom connects the scale feed bin by closed conduit; be provided with controlled valve between intermediate bunker and the scale feed bin simultaneously; the scale feed bin is equipped with the Weightlessness balance of raw materials weighing, and each scale bin bottom is connected with two-rotor continuous mixer by closed conduit again.Auxiliary agent feed bin in the described raw material cabin is connected with the high-speed mixer that first auxiliary agent is diluted by conveyance conduit, described auxiliary agent is diluted is exactly first auxiliary agent and part polyolefin carrier resin to be pre-mixed, the mixed material material auxiliary agent enters the auxiliary agent feed bin, avoided like this adhesion of auxiliary agent in high-speed mixer and conveyance conduit, be conducive to the conveying of auxiliary agent and the stability of course of conveying, simultaneously so that auxiliary agent is prepared and weighing error reduces; Because raw material time of staying in two-rotor continuous mixer is short, utilizes auxiliary agent preparation technique of the present invention and conveying technology, can make that auxiliary agent is easier to be dispersed in the matrix resin quickly and evenly.
Embodiment 1:
78.8 parts of composition of raw materials: HDPE (MFR=5g/10min under the 190 ℃ * 2.16kg condition), 20 parts of carbon blacks, two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant is 0.2 part, 2,0.3 part in 2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, 0.5 part of calcium stearate, fluoropolymer additive (Dynamar TMPPA) 0.2 part.
The preparation method:
With two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, calcium stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 5min with the HDPE resin by 0.2:0.3:0.5:0.2:10 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 3min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 42 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 75 ℃, fluxing zone and head temperature during at 190 ℃ at 175 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 20% gradually by 0% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 500rpm by 300rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 19.8%, 1.5 grades of carbon black dispension degrees, moisture content 0.08%, oxidation induction period (210 ℃) 75.2min, melt flow rate (MFR) (190 ℃, 21.6kg) 52.4g/10min
Embodiment 2:
68.3 parts of composition of raw materials: HDPE (MFR=16g/10min under the 190 ℃ * 2.16kg condition), 30 parts of carbon blacks, two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant is 0.3 part, 4,0.3 part in 4 '-thiobis (the 6-tert-butyl group-3-methylphenol) antioxidant, 0.5 part of calcium stearate, 0.3 part of zinc stearate, fluoropolymer additive (Dynamar TMPPA) 0.3 part.
The preparation method:
With two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 4,4 '-thiobis (the 6-tert-butyl group-3-methylphenol) antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 6min with the HDPE resin by 0.3:0.3:0.5:0.3:0.3:10 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 4min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 75 ℃, fluxing zone and head temperature during at 195 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 30% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 480rpm by 300rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 30.3%, 1.5 grades of carbon black dispension degrees, moisture content 0.08%, oxidation induction period (210 ℃) 87.5min, melt flow rate (MFR) (190 ℃, 21.6kg) 48.4g/10min
Embodiment 3:
58.9 parts of composition of raw materials: HDPE (MFR=18g/10min under the 190 ℃ * 2.16kg condition), 40 parts of carbon blacks, tricresyl phosphite (2, the 4-di-tert-butyl-phenyl) ester antioxidant is 0.3 part, 2,0.2 part in 2 methylene-two (4-methyl-6-tert-butylphenol) antioxidant, 0.4 part of calcium stearate, fluoropolymer additive (Dynamar TMPPA) 0.2 part.
The preparation method:
With tricresyl phosphite (2,4-di-tert-butyl-phenyl) ester antioxidant, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, calcium stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 3min with the HDPE resin by 0.3:0.2:0.4:0.2:5.5 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 3min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 80 ℃, fluxing zone and head temperature during at 200 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 40% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 450rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 50rpm.
The black masterbatch performance: content of carbon black 39.9%, 1.5 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 75.0min, melt flow rate (MFR) (190 ℃, 21.6kg) 28.7g/10min
Embodiment 4:
28.4 parts of composition of raw materials: HDPE (MFR=10g/10min under the 190 ℃ * 2.16kg condition), 30 parts of HDPE (MFR=30g/10min under the 190 ℃ * 2.16kg condition), 40 parts of carbon blacks, 0.2 part in two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 2,0.2 part in 2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, 0.4 part of calcium stearate, 0.4 part of zinc stearate, fluoropolymer additive (Dynamar TMPPA) 0.4 part.
The preparation method:
With two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 5min with the HDPE resin by 0.2:0.2:0.4:0.4:0.4:8.4 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 3min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 42 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after the HDPE of two kinds of different melt flow rates, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 78 ℃, fluxing zone and head temperature during at 195 ℃ at 175 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 40% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 480rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 40.1%, 1.5 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 62.7min, melt flow rate (MFR) (190 ℃, 21.6kg) 33.9g/10min
Embodiment 5:
42.4 parts of composition of raw materials: HDPE (MFR=18g/10min under the 190 ℃ * 2.16kg condition), 16 parts of LLDPE (MFR=40g/10min under the 190 ℃ * 2.16kg condition), 40 parts of carbon blacks, 0.3 part in two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, β-(4-hydroxy phenyl-3, the 5-di-t-butyl) the positive octadecanol ester of propionic acid antioxidant is 0.3 part, 0.5 part of calcium stearate, 0.3 part of barium stearate, fluoropolymer additive (Dynamar TMPPA) 0.2 part.
The preparation method:
With two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, β-(4-hydroxy phenyl-3,5-di-t-butyl) positive octadecanol ester of propionic acid antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 5min with the LLDPE resin by 0.3:0.3:0.5:0.3:0.2:16 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 3min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 42 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 75 ℃, fluxing zone and head temperature during at 200 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 40% gradually by 30% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 500rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 40.3%, 1.5 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 98.2min, melt flow rate (MFR) (190 ℃, 21.6kg) 45.1g/10min
Embodiment 6:
53.5 parts of composition of raw materials: HDPE (MFR=25g/10min under the 190 ℃ * 2.16kg condition), EVA (MFR=5g/10min under the 190 ℃ * 2.16kg condition, VA content is 5%) 5 parts, 40 parts of carbon blacks, tricresyl phosphite (2, the 4-di-tert-butyl-phenyl) ester antioxidant is 0.3 part, 0.3 part of β-(4-hydroxy phenyl-3,5-di-t-butyl) positive octadecanol ester of propionic acid antioxidant, 0.3 part of calcium stearate, 0.3 part of zinc stearate, fluoropolymer additive (Dynamar TMPPA) 0.3 part.
The preparation method:
With tricresyl phosphite (2,4-di-tert-butyl-phenyl) ester antioxidant, β-(4-hydroxy phenyl-3,5-di-t-butyl) positive octadecanol ester of propionic acid antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 4min with HDPE, EVA resin by 0.3:0.3:0.3:0.3:0.3:7:5 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 4min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 80 ℃, fluxing zone and head temperature during at 200 ℃ at 175 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 40% gradually by 30% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 450rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 39.6%, 1.5 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 95.7min, melt flow rate (MFR) (190 ℃, 21.6kg) 40.5g/10min
Embodiment 7:
43 parts of composition of raw materials: HDPE (MFR=25g/10min under the 190 ℃ * 2.16kg condition), 10 parts of LLDPE (MFR=40g/10min under the 190 ℃ * 2.16kg condition), 45 parts of carbon blacks, 0.4 part in two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, β-(4-hydroxy phenyl-3, the 5-di-t-butyl) the positive octadecanol ester of propionic acid antioxidant is 0.4 part, 0.4 part of calcium stearate, 0.4 part of barium stearate, fluoropolymer additive (Dynamar TMPPA) 0.4 part.
The preparation method:
With two (2,4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, β-(4-hydroxy phenyl-3,5-di-t-butyl) positive octadecanol ester of propionic acid antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 6min with the LLDPE resin by 0.4:0.4:0.4:0.4:0.4:10 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 2min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 42 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 80 ℃, fluxing zone and head temperature during at 205 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 45% gradually by 30% when beginning to feed intake; the two-rotor continuous mixer rotating speed is increased in the 480rpm. two-rotor continuous mixer by 200rpm gradually that the material after the blend is extruded through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 44.7%, 2 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 〉=120min, melt flow rate (MFR) (190 ℃, 21.6kg) 35.8g/10min
Embodiment 8:
18.2 parts of composition of raw materials: HDPE (MFR=25g/10min under the 190 ℃ * 2.16kg condition), 20 parts of HDPE (MFR=18g/10min under the 190 ℃ * 2.16kg condition), 10 parts of LLDPE (MFR=40g/10min under the 190 ℃ * 2.16kg condition), 50 parts of carbon blacks, tricresyl phosphite (2, the 4-di-tert-butyl-phenyl) ester antioxidant is 0.3 part, β-(4-hydroxy phenyl-3, the 5-di-t-butyl) the positive octadecanol ester of propionic acid antioxidant is 0.3 part, 0.3 part in pentaerythrite four (3-lauryl thiopropionate) antioxidant, 0.4 part of calcium stearate, 0.3 part of zinc stearate, 0.2 part of barium stearate, fluoropolymer additive (Dynamar TMPPA) 0.5 part.
The preparation method:
With tricresyl phosphite (2, the 4-di-tert-butyl-phenyl) ester antioxidant, β-(4-hydroxy phenyl-3,5-di-t-butyl) positive octadecanol ester of propionic acid antioxidant, pentaerythrite four (3-lauryl thiopropionate) antioxidant, calcium stearate, zinc stearate, barium stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 4min with the LLDPE resin by 0.3:0.3:0.3:0.4:0.3:0.2:0.5:10 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 4min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 85 ℃, fluxing zone and head temperature during at 205 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 50% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 480rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 65rpm.
The black masterbatch performance: content of carbon black 49.4%, 2.5 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 94.9min, melt flow rate (MFR) (190 ℃, 21.6kg) 32.1g/10min
Embodiment 9:
27 parts of composition of raw materials: HDPE (MFR=25g/10min under the 190 ℃ * 2.16kg condition), 15 parts of LLDPE (MFR=40g/10min under the 190 ℃ * 2.16kg condition), 55 parts of carbon blacks, two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant is 0.4 part, 2,0.4 part in 2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, 0.2 part in pentaerythrite four (3-lauryl thiopropionate) antioxidant, 1.0 parts of calcium stearates, 0.5 part of zinc stearate, fluoropolymer additive (Dynamar TMPPA) 0.5 part.
The preparation method:
With two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, pentaerythrite four (3-lauryl thiopropionate) antioxidant, calcium stearate, zinc stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 4min with the LLDPE resin by 0.4:0.4:0.2:1.0:0.5:0.5:15 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 4min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 85 ℃, fluxing zone and head temperature during at 210 ℃ at 185 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 55% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 400rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 55rpm.
The black masterbatch performance: content of carbon black 54.4%, 3 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 〉=120min, melt flow rate (MFR) (190 ℃, 21.6kg) 21.3g/10min
Embodiment 10:
12.3 parts of composition of raw materials: HDPE (MFR=25g/10min under the 190 ℃ * 2.16kg condition), 20 parts of LLDPE (MFR=50g/10min under the 190 ℃ * 2.16kg condition), EVA (MFR=5g/10min under the 190 ℃ * 2.16kg condition, VA content is 14%) 10 parts, 55 parts of carbon blacks, two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant is 0.4 part, 2,0.4 part in 2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, 0.8 part of calcium stearate, 0.4 part of zinc stearate, 0.2 part of barium stearate, fluoropolymer additive (Dynamar TMPPA) 0.5 part.
The preparation method:
With two (2, the 4-di-tert-butyl-phenyl) pentaerythritol diphosphites antioxidant, 2,2 ' methylene-two (4-methyl-6-tert-butylphenol) antioxidant, calcium stearate, zinc stearate, barium stearate, fluoropolymer additive (Dynamar TMPPA) below 500rpm, stir 4min with LLDPE, EVA resin by 0.4:0.4:0.8:0.4:0.2:0.5:3.5:10 namely controls mixer under low-speed conditions in high-speed mixer rotating speed, then start rotating speed that high-speed stirred namely controls mixer can discharge behind the above 4min of 1000rpm to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ℃ can discharge to the auxiliary agent feed bin.
Agent mixture after HDPE, LLDPE carbon black and the dilution drops into separately in the feed bin stand-by.The temperature stabilization for the treatment of two-rotor continuous mixer, is opened integrated feeding system and various materials are sent is caused two-rotor continuous mixer at 85 ℃, fluxing zone and head temperature during at 210 ℃ at 180 ℃, single screw extrusion machine transportation section temperature; Content of carbon black is promoted to 55% gradually by 20% when beginning to feed intake, and the two-rotor continuous mixer rotating speed is increased to 420rpm by 200rpm gradually.Material in the two-rotor continuous mixer after the blend extrudes through single screw extrusion machine again and through the pelleter granulation, screw speed is 45rpm.
The black masterbatch performance: content of carbon black 54.7%, 3 grades of carbon black dispension degrees, moisture content 0.10%, oxidation induction period (210 ℃) 〉=120min, melt flow rate (MFR) (190 ℃, 21.6kg) 21.6g/10min.

Claims (4)

1. the preparation system device of a high-performance carbon black masterbatch; it is characterized in that: this device includes raw material cabin; integrated feeding system; two-rotor continuous mixer; single screw extrusion machine and pelleter; described integrated feeding system is comprised of n dynamic weighting system; each dynamic weighting system all has intermediate bunker; scale feed bin and Weightlessness balance form; the intermediate bunker top is by sealing conveyance conduit and the connection of corresponding raw material cabin; intermediate bunker also is connected with vavuum pump by closed conduit; the intermediate bunker bottom connects the scale feed bin by closed conduit; be provided with controlled valve between intermediate bunker and the scale feed bin simultaneously; the scale feed bin is equipped with the Weightlessness balance of raw materials weighing; each scale bin bottom is connected with two-rotor continuous mixer by closed conduit again, and wherein n quantity is less than or equal to the quantity of using the raw material number in the prescription.
2. the preparation system device of high-performance carbon black masterbatch according to claim 1, it is characterized in that the auxiliary agent feed bin in the described raw material cabin is connected with the high-speed mixer that can first auxiliary agent be diluted by conveyance conduit, described auxiliary agent is diluted is exactly first auxiliary agent and part polyolefin carrier resin to be pre-mixed, and mixed material enters the auxiliary agent feed bin.
3. the preparation system device of high-performance carbon black masterbatch according to claim 1, the control method that it is characterized in that described dynamic weighting system is independent control method or interlock control method, wherein said independent control method is that each weighing subsystem arranges the value of feeding intake by prescription, and independently feeds intake; Described interlock control method is namely set the prescription value of the dynamic weighting system of one of them raw material, the dynamic weighting system of other raw material is according to the actual value of feedback that feeds intake of prescription value of that dynamic weighting system that claims to have set, press formula rate, corresponding adjustment inventory.
4. the preparation system device of a use such as the arbitrary described high-performance carbon black masterbatch of claim 1-3 prepares the method for high-performance carbon black masterbatch, it is characterized in that may further comprise the steps:
Auxiliary agent dilution and mixed at high speed: in high-speed mixer with part polyolefin carrier resin and dispersant in the formula material, processing aid and antioxidant mix, polyolefin carrier resin demand in its high-speed mixer: auxiliary dosage quality proportioning is 5～10: 1, mixed method is that the rotating speed of namely controlling high-speed mixer under the first low-speed conditions stirs 3～8min below 500rpm, then start high-speed stirred and namely control the rotating speed of high-speed mixer more than 1000rpm, get final product discharge behind high-speed stirred 2～5min to the water-cooled mixer of another jacketed, compound continues to mix in the water-cooled mixer of jacketed, when drop in temperature to 40 ± 5 ℃ can discharge to the auxiliary agent feed bin;
Integrated material loading and Dynamic Weighting: open integrated feeding system, in intermediate bunker, form vacuum by vavuum pump, the auxiliary agent of the pressure differential of utilizing intermediate bunker and raw material cabin after with carbon black, polyolefin carrier resin, dilution is delivered to the intermediate bunker of dynamic weighting system, various raw materials are continuously directly put into behind the Weightlessness balance automatic gauge in the scale feed bin and are carried out blend in the two-rotor continuous mixer, wherein the two-rotor continuous mixer rotating speed is controlled at 200～550rpm, temperature is at 170～190 ℃, production capacity 200～400kg/h;
The single screw extrusion machine granulation: the material in the two-rotor continuous mixer after the blend is extruded and through the pelleter granulation through single screw extrusion machine again; wherein single screw extrusion machine transportation section temperature is controlled at 70～100 ℃; fluxing zone and head temperature are controlled at 180～220 ℃; screw speed is 40～80rpm, production capacity 200～400kg/h.
CN201210390855.0A 2011-04-01 2011-04-01 Preparation system device and preparation method for high-performance black master-batches Expired - Fee Related CN102922618B (en)

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CN105710987A (en) * 2016-04-20 2016-06-29 江苏通用科技股份有限公司 Graphene-oil processing and feeding equipment of banbury mixer
CN106113309A (en) * 2016-08-18 2016-11-16 四川远星橡胶有限责任公司 A kind of banbury with feeding device
CN111004427A (en) * 2019-12-20 2020-04-14 山东东宏管业股份有限公司 HDPE carrier carbon black master batch for PE pressure pipeline and preparation method thereof
CN111639435A (en) * 2020-06-04 2020-09-08 青岛科技大学 Banbury mixer rotor energy consumption prediction method for bolt lifting action in rubber mixing process

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