CN104589523A - Production method and production equipment of special material for polypropylene melt-blown non-woven fabric - Google Patents
Production method and production equipment of special material for polypropylene melt-blown non-woven fabric Download PDFInfo
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- CN104589523A CN104589523A CN201510023201.8A CN201510023201A CN104589523A CN 104589523 A CN104589523 A CN 104589523A CN 201510023201 A CN201510023201 A CN 201510023201A CN 104589523 A CN104589523 A CN 104589523A
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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
- B29C48/88—Thermal treatment of the stream of extruded material, e.g. cooling
- B29C48/919—Thermal treatment of the stream of extruded material, e.g. cooling using a bath, e.g. extruding into an open bath to coagulate or cool the material
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Abstract
The invention discloses a production method and production equipment of a special material for a polypropylene melt-blown non-woven fabric. The production method comprises the following steps: adding 50-200g of a long-acting stabilizing agent, 25-200g of a short-acting stabilizing agent, 25-160g of a high-temperature-resistant stabilizing agent and 20-100g of a lubricating agent to each 100kg of polypropylene; and mixing by using a mixing machine, and discharging to an extruder, and generating a reaction in a lead-screw reaction section of a double-screw extruder. The production equipment comprises a mixing machine, wherein uniformly mixed raw materials are discharged into an intermediate bunker from a mixed material outlet, an outlet in the bottom of the intermediate bunker is connected with an inlet of the extruder, the extruder is of a dual-screw structure and is used for sending processed materials to a cooling water tank for being cooled by virtue of an inclined water tank, then air-dried by an air dryer, granulated in a granulating machine, screened by a vibrating screen, and sent into a homogenizing and mixing tank by virtue of a rotary discharging device. The production method and the production equipment have the beneficial effects of uniformly mixing the raw materials and solving the difficulty of forming of polypropylene with a high flowing melting index, and are suitable for conventional production.
Description
Technical field
The invention belongs to nonwoven production technical field, relate to a kind of polypropylene melt blown non-woven fabric PP Pipe Compound production method and production equipment.
Background technology
Melt spraying non-woven fabrics belongs to the one of non-weaving cloth.Due to the uniqueness of melt-blown process, the fiber making it produce is close to superfine fibre, thus melt spraying non-woven fabrics has excellent obstruct filterability, gas permeability, oil absorption, is widely used in the fields such as medical protection, sanitary cleaning material, filtering material, warming wadding material, oil absorption material, battery separator.Mainly contain Korea S great Lin in the market to expect, melt finger and accomplish 900g/10min, 1500g/10min, the 1200/10min of Borealis, EXXONMOBIL have PP3505G (melt and refer to 400g/10min), PP3546G (melt and refer to 1200g/10min), PP3746G (melt and refer to 1500g/10min).
Domestic due to technology immature, the producer producing melt-blown material is considerably less, and product poor fluidity, melts and refer to unstable and content of ashes is high, has peculiar smell, is thus difficult to be easily accepted by a user.Domestic Yang Zi chemical research institute, Down, Longkou, Shanghai Yi Shitong, middle section spulon has melt-blown material, but user is reflected that domestic material has to melt and referred to that fluctuation is large, the shortcomings such as easy blocking sprayer, and melts finger and can only accomplish 1500g/10min.
The preparation technology of this PP Pipe Compound is roughly divided into two kinds, and one is chemical degradation method, and is divided into degradable method and incomplete edman degradation Edman, domesticly at present generally adopts incomplete edman degradation Edman.Another kind is that metallocene catalyst direct polymerization forms, the melt-blown material that this method obtains has fabulous processing stability, the fiber compliance produced is better, but the processing cost of this method is higher, no matter be therefore that import or domestic material adopt chemical degradation method to produce mostly at present.
Summary of the invention
The object of the present invention is to provide a kind of high-end polypropylene melt spraying non-woven fabrics PP Pipe Compound production method, solve raw and auxiliary material and degradation agent undercompounding when reacting in existing technology production process, reaction time is inadequate, cause product melting means unstable, molecular weight distribution is wide, is not suitable for melt-spraying spinning technique; And die head and water trough design improper, the problem of difficult forming.
The technical solution adopted in the present invention is carried out according to following steps:
Step 1, preparation raw material: every 100 kilograms of polypropylene, add long-acting stabilizing agent 50-200 gram, fugitive stabilizing agent 25-200 gram, heat-resistant stable agent 25-160 gram, lubricant 20-100 gram;
Step 2, above-mentioned raw materials is put into mixer mix, mixer mixing speed 40-100 rev/min, stir 10-45 minute, whipping temp is 0-40 DEG C, obtains raw mixture after stirring;
Step 3: store for future use under raw mixture to intermediate bunker.Intermediate bunker connects double screw extruder blanking tube, expects extruder under even by feeding machine;
Step 4: degradation agent BIPB, DTBP, one or more mixing of DCP are by degradation agent pump accurate-metering, addition is 1 ~ 8 ‰ of raw mixture, inject at double screw extruder degradation agent inlet continuous uniform, raw mixture and degradation agent, at the temperature of 160 DEG C ~ 280 DEG C, react in the spiro rod reaction section of double screw extruder;
Step 5: the melt polypropylene becoming high fusion index at the polypropylene of the conversion zone low melt index of extruder, flow out from extruder die head, guide through oblique tank and flow into bosh, flowing normal temperature cooling water in bosh, strip melt cooling forming in bosh, through the air-dry laggard pelleter pelletizing of air-dry machine, after vibratory sieve removes bulk sizing and tiny particle, particle sends into homogenizing blending tank through blast system;
Step 6: particle completes homogenizing and the taste that degass in homogenizing blending tank, finally sends into finished pot and is packaged into product by weight.
Further, described polypropylene is the polypropylene of melting means in the low melt index of 0.5-50; Described long-acting stabilizing agent be stabilizing agent 1076 or/and stabilizing agent 1010, fugitive stabilizing agent be stabilizing agent 168 or/and stabilizing agent 626, heat-resistant stable agent is that stabilizing agent 4001 is or/and stabilizing agent 802; Described lubricant is that Hydrotalcite is or/and calcium stearate.
Polypropylene melt blown non-woven fabric PP Pipe Compound production equipment, comprise mixer, mixer is provided with raw material and auxiliary material entrance and compound and exports, compound outlet is just to the upper entrance of the intermediate bunker of below, the raw material mixed is from compound outlet down in intermediate bunker, the outlet at bottom connecting extruder entrance of intermediate bunker, extruder is double-screw structure, extruder connects delivery pump, degradation agent is sent in extruder by delivery pump, outlet of extruder connects oblique tank, the material processed is sent on the oblique water plate of oblique tank by outlet of extruder, thus make material flow in bosh, oblique tank also provides cooling water to bosh, cooled material is sent in air-dry machine air-dry by conveyer belt by bosh, sending into pelletizing in pelleter by conveyer belt, material after pelletizing is sent into vibratory sieve and is screened by pelleter, and through over-rotation blanking device after blower fan dries up, material is sent in homogenizing blending tank, inside homogenizing blending tank, homogenizing is sent in finished pot after processing and is made finished product.
Further, described extruder comprises mair motor, mair motor is arranged on support, the twin-screw of mair motor by installing in shaft coupling connection for transmission case, transmission case connector drum, twin-screw is placed in cylindrical shell, blanking tube is provided with above cylindrical shell, feeding machine is connected bottom blanking tube, feeding machine is also connected with feeding motor, feeding motor is connected with reductor, feeding machine material outlet connector drum, by feeding machine, the material in blanking tube is sent in cylindrical shell, cylindrical shell is also provided with degradation agent inlet, cylindrical shell is provided with exhaust chamber near terminal, cylindrical shell between exhaust chamber and head is provided with heating watt, cylindrical shell terminal connects net-changing device, net-changing device connects head, head is provided with die head, the fluid foods processed flows out from die head.Net-changing device is supported by support.
Further, described head is arranged downwards for bending, horn mouth cavity in head and the formation fluid passage, screw rod chamber in cylindrical shell, die openings obliquely, the horn mouth cavity of head is the tubaeform of flat, horn mouth cavity oral area is provided with row's aperture, can equal control rate of flow of fluid by aperture.
Further, described oblique tank comprises rectangular box body, and box body side is provided with water inlet, box body is divided into two parts by flow-stopping plate, cassette upper end oral area is provided with to be tilted to down and stretches to outside oblique water plate, and the fluid stream that extruder flows out flows to below after oblique water plate, and box body is supported by leg.
When the invention has the beneficial effects as follows reaction, raw and auxiliary material fully mixes, and reacts completely, and product melting means is stablized, and molecular weight distribution is suitable, is applicable to melt-spraying spinning technique; The particular design of die head and tank, solves the polyacrylic shaping difficult problem of high flow melt index, is applicable to conventional production.
Accompanying drawing explanation
Fig. 1 is polypropylene melt blown non-woven fabric PP Pipe Compound production equipment schematic diagram of the present invention;
Fig. 2 is extruder structure schematic diagram of the present invention;
Fig. 3 is cross-head partial schematic diagram of the present invention;
Fig. 4 is the oblique tank schematic diagram of the present invention;
Fig. 5 is homogenizing blending tank schematic diagram of the present invention.
In figure, 1. mixer, 2. intermediate bunker, 3. extruder, 4. delivery pump, 5. oblique tank, 6. bosh, 7. air-dry machine, 8. pelleter, 9. vibratory sieve, 10. blower fan, 11. rotating blanking apptss, 12. homogenizing blending tanks, 13. finished pots, 101. auxiliary material entrances, 102. compound outlets, 301. mair motor, 302. support, 303. shaft coupling, 304. transmission case, 305. feeding motor, 306. reductor, 307. blanking tube, 308. feeding machine, 309. degradation agent inlets, 310. twin-screw, 311. cylindrical shell, 312. exhaust chamber, 313. heating watt, 314. net-changing device, 315. head, 316. die head, 317. support, 318. horn mouth cavitys, 319. aperture, 501. water inlet, 502. flow-stopping plate, 503. oblique water plates, 504. box body, 505. leg, 1201. charging aperture, 1202. homogenizing pipe.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
The object of the invention is to propose a kind of realization on the basis of low cost and melt by low the method referring to polypropylene long period steady production high-quality polypropylene melt-blown PP Pipe Compound.The technology path that the present invention adopts is the complete controlled degradation route of polypropylene, makes low melting refer to that polypropylene and degradation agent react completely in the extruder of particular design by adding degradation agent, makes polypropylene be changed into height melted finger by the low finger that melts.
The inventive method step:
Step 1, preparation raw material: every 100 kilograms of polypropylene, add long-acting stabilizing agent 50-200 gram, fugitive stabilizing agent 25-200 gram, heat-resistant stable agent 25-160 gram, lubricant 20-100 gram;
Step 2, above-mentioned raw materials is put into mixer mix, mixer mixing speed 40-100 rev/min, stir 10-45 minute, whipping temp is 0-40 DEG C, obtains raw mixture after stirring; Polypropylene is the polypropylene of melting means in the low melt index of 0.5-50.Long-acting stabilizing agent be stabilizing agent 1076 or/and stabilizing agent 1010, fugitive stabilizing agent be stabilizing agent 168 or/and stabilizing agent 626, heat-resistant stable agent is that stabilizing agent 4001 is or/and stabilizing agent 802.Lubricant is that Hydrotalcite is or/and calcium stearate.
Step 3: store for future use under raw mixture to intermediate bunker.Intermediate bunker connects double screw extruder blanking tube, expects extruder under even by feeding machine;
Step 4: degradation agent BIPB, DTBP, one or more mixing of DCP are by degradation agent pump accurate-metering, addition is 1 ~ 8 ‰ of raw mixture, inject at double screw extruder degradation agent inlet continuous uniform, raw mixture and degradation agent, at the temperature of 160 DEG C ~ 280 DEG C, react in the spiro rod reaction section of double screw extruder;
Step 5: the melt polypropylene becoming high fusion index at the polypropylene of the conversion zone low melt index of extruder, flow out from extruder die head, guide through oblique tank and flow into bosh, flowing normal temperature cooling water in bosh, strip melt cooling forming in bosh, through the air-dry laggard pelleter pelletizing of air-dry machine, after vibratory sieve removes bulk sizing and tiny particle, particle sends into homogenizing blending tank through blast system;
Step 6: particle completes homogenizing and the taste that degass in homogenizing blending tank, finally sends into finished pot and is packaged into product by weight.
The product polypropylene melt-blown PP Pipe Compound that the inventive method is produced, belongs to one of raw material of melt spraying non-woven fabrics.PP Pipe Compound of the present invention is easily processed, and has good mesh sheet mouldability, cohesive, low color, odorless, excellent stability and compatibility, good economy.Because domestic material effect is undesirable on domestic market, melt-blown material 90% is import.And adopt polypropylene melt-blown PP Pipe Compound of the present invention can change this phenomenon.
Polypropylene melt blown non-woven fabric PP Pipe Compound production equipment, as shown in Figure 1, comprise mixer 1, mixer 1 is provided with raw material and auxiliary material entrance 101 and compound and exports 102, compound outlet 102 is just to the upper entrance of the intermediate bunker 2 of below, the raw material mixed is from compound outlet 102 down in intermediate bunker 2, outlet at bottom connecting extruder 3 entrance of intermediate bunker 2, extruder 3 is double screw extruder, extruder 3 connects delivery pump 4, degradation agent is sent in extruder 3 by delivery pump 4, extruder 3 exports and connects oblique tank 5, the material processed is exported by extruder 3 on the oblique water plate 501 sending into oblique tank 5, thus make material flow in bosh 6, oblique tank 5 also provides cooling water to bosh 6, cooled material is sent in air-dry machine 7 air-dry by conveyer belt by bosh 6, sending into pelletizing in pelleter 8 by conveyer belt, material after pelletizing is sent into vibratory sieve 9 and is screened by pelleter 8, and through over-rotation blanking device 11 after blower fan 10 dries up, material is sent in homogenizing blending tank 12, inside homogenizing blending tank 12, homogenizing is sent in finished pot 13 after processing and is made finished product.
As shown in Figure 2, extruder 3 comprises mair motor 301, mair motor is arranged on support 302, the twin-screw 310 of mair motor 301 by installing in shaft coupling 303 connection for transmission case 304, transmission case connector drum 311, twin-screw 310 is placed in cylindrical shell 311, blanking tube 307 is provided with above cylindrical shell 311, feeding machine 308 is connected bottom blanking tube 307, feeding machine 308 is also connected with feeding motor 305, feeding motor 305 is connected with reductor 306, feeding machine 308 material outlet connector drum 311, by feeding machine 308, the material in blanking tube 307 is sent in cylindrical shell 311, cylindrical shell 311 is also provided with degradation agent inlet 309, cylindrical shell 311 is provided with exhaust chamber 312 near terminal, cylindrical shell 311 between exhaust chamber 312 and head 315 is provided with and heats watts 313, cylindrical shell 311 terminal connects net-changing device 314, net-changing device 314 connects head 315, head 315 is provided with die head 316, the fluid foods processed flows out from die head 316.Net-changing device 314 is supported by support 317.
Be extruder 3 head section structure as shown in fig. 3 a-c, Fig. 3 a is head section sectional view, described head 315 is arranged downwards for bending, horn mouth cavity 318 in head and the formation fluid passage, screw rod chamber in cylindrical shell 311, obliquely, the horn mouth cavity 318 of head 315 is the tubaeform of flat to die head 316 opening.Fig. 3 b is top view; Fig. 3 c is horn mouth cavity 318 schematic diagram, and described horn mouth cavity 318 oral area is provided with row's aperture 319, can equal control rate of flow of fluid by aperture 319.
As shown in Figure 4, described oblique tank 5 comprises rectangular box body 504, box body 504 side is provided with water inlet 501, box body 504 is divided into two parts by flow-stopping plate 502, box body 504 upper end oral area is provided with to be tilted to down and stretches to outside oblique water plate 503, the fluid stream that extruder 3 flows out flows to below after oblique water plate 503, and box body 504 is supported by leg 505.Bosh is long 7000mm preferably, wide 500mm, dark 300mm.
Be homogenizing blending tank 12 structure as shown in Figure 5 a, described homogenizing blending tank 12 top is charging aperture 1201, and the inside is provided with four homogenizing pipes 1202.Four homogenizing pipe 1202 upper end orifice are also connected with the pipeline of rotating blanking appts 11.The pipeline of homogenizing blending tank 12 lower end outlet is also communicated with end interface on four homogenizing pipes 1202, can realize material like this and circulate homogenizing at homogenizing blending tank 12.The piping arrangement in homogenizing blending tank 12 cross section as shown in Figure 5 b.
The design of degradation agent inlet 309, to ensure that degradation agent mixes and the reaction time with polyacrylic, near control degradation agent inlet 309, the temperature of double screw extruder bringing-up section, at 40 ~ 180 DEG C, prevents inlet from blocking, affects the injection that degradation agent is uniform and stable simultaneously.
The design of special chain-drive section, the die head 316 of double screw extruder facilitates high particular design of melting the constant slope referring to polypropylene melt flow by universal being designed to, namely the angle of orifice exit and vertical direction is between 0 ~ 45 °, guarantee that the low viscous melt of high flowing enters oblique tank 5, cooling and shaping as early as possible.Melt polypropylene, through screw rod chamber, is distributed to head 315 after net-changing device 314, then is flowed out by 15 ~ 25 apertures 319 that die head 316 is horizontal, and aperture 319 is nib, imports oblique tank 5, rapid cooling forming by oblique water plate 503.The angle design of extruder 3 die head 316 and the design of oblique tank 5 are worked in coordination, and object can be cooled rapidly after melt polypropylene is flowed out stably, facilitates shaping check rod.
From the melt polypropylene that the die head 316 of extruder 3 flows out, first oblique tank 5 is touched, oblique tank 5 is designed to certain gradient, through stable source of water process, there is provided and relax stable water source and melt with high the angle referring to fluid contact, completely solve the problem that super-high fluidity melt polypropylene is difficult to cooling forming, realize routinizing production, and make melt index be up to 2000g/10min, fully meet the demand of market to high-end polypropylene melt-blown PP Pipe Compound.
Oblique tank 5 is formed primarily of two large parts, water tank box body 504 and flow-stopping plate 502.Water tank box body 504 is the cuboids erect, and upper end is uncovered, lower end closed, and there is water inlet 501 at the back side.Box body 504 is of a size of 365 × 100 × 525, and lower end has two can regulate uneven leg 505, is provided with flow-stopping plate 502, steadily can cushions current in box body 504.The effect of water tank box body 504 current needing to lead thing is introduced box body 504 from water source carry out buffered, is uniformly distributed at the uniform velocity is spilled over to oblique water plate 503 from upper end.The long 600mm of oblique water plate 503, oblique water plate 503 one end connects with a long limit of water tank box body 504 upper end, so width is consistent with the long limit of water tank box body 504, all there is baffle plate on both sides, oblique water plate 503 long limit, composition guiding gutter.The effect of this design be to transport almost vertical and under diversed body time, one is that inclined-plane can shorten the vertically descending distance of diversed body as far as possible, two is that the inclined-plane operating path of fluid after contacting with water can increase initial cool time, be convenient to shaping as early as possible, the initial cooling forming of fluid is most important, is the key of whole forming step.Water guide swash plate need reach certain fineness, and coarse panel may change the flow direction of water, causes water surface movement disorder, affects the intact shaping of diversed body, and this is also the key made.
After the cooling of melt polypropylene check rod, pelletizing enters homogenizing blending tank 12, and product aftertreatment technology adopts homogenizing tank design, from the mixed mode of ginseng and time guarantee to melt refer to evenly, there is no smell, reach the requirement of medicine and hygiene fields preferably.
Polypropylene is the polymer of heat-resisting oxygen instability, repeatedly adds color and mechanical property that trade union affects its goods, therefore all uses the stabilizing agent of difference in functionality in process and goods, to stablize its processing and serviceability.The present invention controls the suitable proportioning of length effect stabilizing agent, increase the stabilizer component of the high temperature of more resistance to spinning simultaneously, control than being, long-acting stabilizing agent: fugitive stabilizing agent: heat-resistant stable agent is 1:(0.5 ~ 1): (0.5 ~ 0.8), ensure that product yellow colour index is less than 1, Downstream processing has good stability.
The present invention will be described to enumerate specific embodiment below.
The production of the melt-blown PP Pipe Compound of embodiment 1:PF1500.
Constant weight melts the polypropylene powder referred to for 30g/10min, and its character is as shown in table 1, and the proportions pressing table 2 with stabilizing agent, lubricant is good, puts into intermediate bunker in mixer after mixing, and becomes polypropylene miser to be processed.Intermediate bunker connects with the loading hopper of double screw extruder.Double screw extruder is pressed table 4 operational factor and is run, degradation agent is added by second to the 3rd section of centre of degradation agent pump at double screw extruder, addition controls in the ratio of degradation agent in table 3 and polypropylene miser, namely the feeding load in table 4 determines the inlet amount of mixture, and the addition of degradation agent regulates by table 3 proportion requirement.Extrude from nib through the reacted melt polypropylene of twin-screw, the air-dry shaping pelletizing of water cooling, wind sends into products pot, and batch carries out being mixed of ginseng in homogenizing tank, becomes product by heavy weighing and bagging.Product property is in table 5.
Table 1 pp material character
Table 2 pp material and additive formula
The proportioning of table 3 polypropylene miser and degradation agent
| Pp material mixture | Degradation agent DCP |
| 100Kg | 300g |
The operational factor of table 4 double screw extruder
| Parameter | Unit | Controlling value |
| Extruder each section of control temperature | ℃ | 160～280 |
| Driving screw rotating speed | Rev/min | 180～400 |
| Feeding load | HZ | 10～30 |
| Vacuum degree control | MPa | -0.08～-0.04 |
| Degradation agent adds load | g/min | 10～30 |
Table 5PF1500 product property
| Product grade | Unit | PF1500 | PF1500 | PF1500 |
| Product batch | Ton | 30 | 30 | 30 |
| Date of manufacture | 2009.4.2 | 2009.01.22 | 2008.06.17 | |
| Melt index | g/10min | 1499 | 1488 | 1478 |
| Yellow colour index | -3.25 | -6.51 | -4.7 | |
| Moisture | ％ | 0.15 | 0.13 | 0.11 |
| Ash content | ppm | 205 | 193 | 217 |
| Molecular weight distribution | ≤3 | ≤3 | ≤3 |
The production of the melt-blown PP Pipe Compound of embodiment 2:PF1200.
It is as shown in table 6 that constant weight melts the polypropylene granules performance that finger is 3g/10min, and the proportions pressing table 7 with stabilizing agent, lubricant is good, puts into intermediate bunker in mixer after mixing, and becomes polypropylene miser to be processed.Intermediate bunker connects with the loading hopper of double screw extruder.Double screw extruder is pressed table 9 operational factor and is run, degradation agent is added by second to the 3rd section of centre of degradation agent pump at double screw extruder, addition controls in the ratio of degradation agent in table 8 and polypropylene miser, namely the feeding load in table 9 determines the inlet amount of mixture, and the addition of degradation agent regulates by table 8 proportion requirement.Extrude from nib through the reacted melt polypropylene of twin-screw, the air-dry shaping pelletizing of water cooling, wind sends into products pot, and batch carries out being mixed of ginseng in homogenizing tank, and become product by heavy weighing and bagging, properties of product are in table 10.
Table 6 pp material character
Table 7 pp material and additive formula,
The proportioning of table 8 polypropylene miser and degradation agent
| Pp material | Degradation agent DCP |
| 100Kg | 250g |
The operational factor of table 9 double screw extruder
| Parameter | Unit | Controlling value |
| Extruder each section of control temperature | ℃ | 160～280 |
| Driving screw rotating speed | Rev/min | 180～400 |
| Feeding load | HZ | 10～30 |
| Vacuum degree control | MPa | -0.08～-0.04 |
| Degradation agent addition | g/min | 10～30 |
Table 10PF1200 product property
| Product grade | Unit | PF1200 | PF1200 | PF1200 |
| Product batch | Ton | 30 | 30 | 30 |
| Date of manufacture | 2009.07.02 | 2009.04.24 | 2009.01.18 | |
| Melt index | g/10min | 1218 | 1224 | 1250 |
| Yellow colour index | -4.84 | -4.64 | -6.68 | |
| Moisture | ％ | 0.2 | 0.16 | 0.07 |
| Ash content | ppm | 150 | 182 | 241 |
| Molecular weight distribution | ≤3 | ≤3 | ≤3 |
The production of the melt-blown PP Pipe Compound of embodiment 3:PF1800.
It is as shown in table 11 that constant weight melts the Properties of Polypropylene that finger is 35g/10min, and the proportions that table 12 pressed by powder and stabilizing agent, lubricant is good, puts into intermediate bunker in mixer after mixing, and becomes polypropylene miser to be processed.Intermediate bunker connects with the loading hopper of double screw extruder.Double screw extruder is pressed table 14 operational factor and is run, degradation agent is added by second to the 3rd section of centre of degradation agent pump at double screw extruder, addition controls in the ratio of degradation agent in table 13 and polypropylene miser, namely the feeding load in table 14 determines the inlet amount of mixture, the addition of degradation agent is undertaken regulating by table 13 proportion requirement and is extruded from nib through the reacted melt polypropylene of twin-screw, the air-dry shaping pelletizing of water cooling, wind sends into products pot, batch carries out being mixed of ginseng in homogenizing tank, become product by heavy weighing and bagging, product property is in table 15.
Table 11 pp material character
Table 12 pp material and additive formula
The proportioning of table 13 polypropylene miser and degradation agent
| Pp material mixture | Degradation agent DTBP |
| 100Kg | 360g |
The operational factor of table 14 double screw extruder
| Parameter | Unit | Controlling value |
| Extruder each section of control temperature | ℃ | 160～280 |
| Driving screw rotating speed | Rev/min | 180～400 |
| Feeding load | HZ | 10～50 |
| Vacuum degree control | MPa | -0.08～-0.04 |
| Degradation agent addition | g/min | 10～40 |
Table 15PF1800 product property
| Product grade | Unit | PF1800 | PF1800 | PF1800 |
| Product batch | Ton | 30 | 30 | 30 |
| Date of manufacture | 2009.04.03 | 2009.10.01 | 2008.12.18 | |
| Melt index | g/10min | 1735 | 1806 | 1756 |
| Yellow colour index | -10.49 | -9.66 | -7.34 | |
| Moisture | ％ | 0.08 | 0.19 | 0.10 |
| Ash content | ppm | 202 | 140 | 188 |
| Molecular weight distribution | ≤3 | ≤3 | ≤3 |
The present invention has following advantage:
The polypropylene melt-blown PP Pipe Compound that the present invention produces, melt index is high, good fluidity, narrow molecular weight distribution, melts and refers to stablize, free from extraneous odour.The course of industrialization of product is integrated with new technology, new formula, new equipment., improve the stability of product, reliability.Product is suitable for import wide cut high speed non-woven fabric production line produces MB cloth, SMS cloth, SMMS cloth.The non-woven fabrics made is soft, good permeability, filterability is excellent, and there is no peculiar smell, obtain the accreditation of downstream client, and filled up domestic blank in high-grade melt spraying non-woven fabrics field, occupy the market of domestic high-end polypropylene melt material spray 70%, relative import material has good cost performance, achieves good economic benefit and social benefit.
Since this method invention, company's this project annual value of production is annual by more than 30% speed increment over nearly 3 years, 09 annual value of production crosses hundred million, is the main raw materials provider of the high-end polypropylene melt-blown nonwoven production manufacturers such as the general outstanding person in Guangdong, south, the South Sea are new, the pretty richness in Shandong, TEDA in Tianjin.
Technical characteristic of the present invention:
A. the starting point of foreign technology is at polymerization stage, have employed expensive new catalyst.The starting point of our technology is placed on the post-modification stage, and the polypropylene of lazy flow is transformed into the melt-blown material of high fluidity in double screw extruder, cost is lower than imported product.
B. import material molecular weight distribution >=3.The design of this invention conversion zone makes reaction more fully more complete, and molecular weight distribution≤3, narrowly distributing, is more suitable for spinning.
C. import material is due to containing unreacted molecular weight regulator, and therefore in storage process, quality easily changes, and therefore import material all can have a shorter shelf-life restriction.
D. the equipment of domestic employing is typical twin screw extruder, and is not exclusively applicable to degradation reaction, and degradation reaction not exclusively and be difficult to control.What this invention adopted is response type double screw extruder, and has carried out special design to screw zones, and degradation reaction can be made more complete.
E. the domestic polyacrylic shaping reference for super-high fluidity is the forming method of polypropylene cooling order grain, namely at a lower temperature, allow reaction not exclusively, the flowing velocity of melt is not high, thus shaping, so certainly will cause the instability problem in the follow-up use of melt-blown material.This invention then adopts novel molded design, is not reducing reaction temperature, when complete reaction, makes the shaping pelletizing of the polypropylene of super-high fluidity.
F. the melt-blown material ubiquity odor problem of domestic manufacturer, does not reach the requirement of medical treatment, health field, limits the application in high-grade non-woven fabrics.Fully taking into account product specification problem in this invention design, is promote quality, and specialized designs last handling process, to have reached the object eliminating smell.
G. the melt index of home products is the highest can only reach 1500g/10min, and the product melt index of this invention can reach 2000g/10min, meets the requirement of high-grade melt-blown material.
The above is only to better embodiment of the present invention, not any pro forma restriction is done to the present invention, every any simple modification done above embodiment according to technical spirit of the present invention, equivalent variations and modification, all belong in the scope of technical solution of the present invention.
Claims (6)
1. a polypropylene melt blown non-woven fabric PP Pipe Compound production method, is characterized in that carrying out according to following steps:
Step 1, preparation raw material: every 100 kilograms of polypropylene, add long-acting stabilizing agent 50-200 gram, fugitive stabilizing agent 25-200 gram, heat-resistant stable agent 25-160 gram, lubricant 20-100 gram;
Step 2, above-mentioned raw materials is put into mixer mix, mixer mixing speed 40-100 rev/min, stir 10-45 minute, whipping temp is 0-40 DEG C, obtains raw mixture after stirring;
Step 3: store for future use under raw mixture to intermediate bunker.Intermediate bunker connects double screw extruder blanking tube, expects extruder under even by feeding machine;
Step 4: degradation agent BIPB, DTBP, one or more mixing of DCP are by degradation agent pump accurate-metering, addition is 1 ~ 8 ‰ of raw mixture, inject at double screw extruder degradation agent inlet continuous uniform, raw mixture and degradation agent, at the temperature of 160 DEG C ~ 280 DEG C, react in the spiro rod reaction section of double screw extruder;
Step 5: the melt polypropylene becoming high fusion index at the polypropylene of the conversion zone low melt index of extruder, flow out from extruder die head, guide through oblique tank and flow into bosh, flowing normal temperature cooling water in bosh, strip melt cooling forming in bosh, through the air-dry laggard pelleter pelletizing of air-dry machine, after vibratory sieve removes bulk sizing and tiny particle, particle sends into homogenizing blending tank through blast system;
Step 6: particle completes homogenizing and the taste that degass in homogenizing blending tank, finally sends into finished pot and is packaged into product by weight.
2., according to polypropylene melt blown non-woven fabric PP Pipe Compound production method a kind of described in claim 1, it is characterized in that: described polypropylene is the polypropylene of melting means in the low melt index of 0.5-50; Described long-acting stabilizing agent be stabilizing agent 1076 or/and stabilizing agent 1010, fugitive stabilizing agent be stabilizing agent 168 or/and stabilizing agent 626, heat-resistant stable agent is that stabilizing agent 4001 is or/and stabilizing agent 802; Described lubricant is that Hydrotalcite is or/and calcium stearate.
3. for the polypropylene melt blown non-woven fabric PP Pipe Compound production equipment of method described in claim 1, it is characterized in that: comprise mixer (1), mixer (1) is provided with raw material and auxiliary material entrance (101) and compound and exports (102), compound outlet (102) is just to the upper entrance of the intermediate bunker (2) of below, the raw material mixed is from compound outlet (102) down in intermediate bunker (2), outlet at bottom connecting extruder (3) entrance of intermediate bunker (2), extruder (3) is double-screw structure, extruder (3) connects delivery pump (4), degradation agent is sent in extruder (3) by delivery pump (4), extruder (3) outlet connects oblique tank (5), the material processed is sent on the oblique water plate (501) of oblique tank (5) by extruder (3) outlet, thus make material flow in bosh (6), oblique tank (5) also provides cooling water to bosh (6), cooled material is sent in air-dry machine (7) air-dry by conveyer belt by bosh (6), being sent into pelletizing in pelleter (8) by conveyer belt, material after pelletizing is sent into vibratory sieve (9) and is screened by pelleter (8), and through over-rotation blanking device (11) after blower fan (10) dries up, material is sent in homogenizing blending tank (12), process in rear feeding finished pot (13) in homogenizing blending tank (12) the inside homogenizing and make finished product.
4. according to polypropylene melt blown non-woven fabric PP Pipe Compound production equipment described in claim 3, it is characterized in that: described extruder (3) comprises mair motor (301), mair motor is arranged on support (302), the twin-screw (310) of mair motor (301) by installing in shaft coupling (303) connection for transmission case (304), transmission case connector drum (311), twin-screw (310) is placed in cylindrical shell (311), cylindrical shell (311) top is provided with blanking tube (307), blanking tube (307) bottom connects feeding machine (308), feeding machine (308) is also connected with feeding motor (305), feeding motor (305) is connected with reductor (306), feeding machine (308) material outlet connector drum (311), by feeding machine (308), the material in blanking tube (307) is sent in cylindrical shell (311), cylindrical shell (311) is also provided with degradation agent inlet (309), cylindrical shell (311) is provided with exhaust chamber (312) near terminal, cylindrical shell (311) between exhaust chamber (312) and head (315) is provided with and heats watt (313), cylindrical shell (311) terminal connects net-changing device (314), net-changing device (314) connects head (315), head (315) is provided with die head (316), the fluid foods processed flows out from die head (316).Net-changing device (314) is supported by support (317).
5. according to polypropylene melt blown non-woven fabric PP Pipe Compound production equipment described in claim 4, it is characterized in that: described head (315) is arranged downwards for bending, horn mouth cavity (318) in head and the formation fluid passage, screw rod chamber in cylindrical shell (311), die head (316) opening obliquely, what the horn mouth cavity (318) of head (315) was flat is tubaeform, horn mouth cavity (318) oral area is provided with row's aperture (319), can equal control rate of flow of fluid by aperture (319).
6. according to polypropylene melt blown non-woven fabric PP Pipe Compound production equipment described in claim 3, it is characterized in that: described oblique tank (5) comprises rectangular box body (504), box body (504) side is provided with water inlet (501), box body (504) is divided into two parts by flow-stopping plate (502), box body (504) upper end oral area is provided with to be tilted to down and stretches to outside oblique water plate (503), the fluid stream that extruder (3) flows out flows to below afterwards oblique water plate (503), and box body (504) is supported by leg (505).
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