CN100579879C - Delivery spray nozzle, polytetrafluoroethylene fine particle processing method and apparatus using the spray nozzle - Google Patents
Delivery spray nozzle, polytetrafluoroethylene fine particle processing method and apparatus using the spray nozzle Download PDFInfo
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- CN100579879C CN100579879C CN200610026921A CN200610026921A CN100579879C CN 100579879 C CN100579879 C CN 100579879C CN 200610026921 A CN200610026921 A CN 200610026921A CN 200610026921 A CN200610026921 A CN 200610026921A CN 100579879 C CN100579879 C CN 100579879C
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Abstract
The invention relates to a method for continuously preparing politef via suspension method, wherein said method breaks, washes, separates, dries and cools the polymerized politef, to obtain middle particles to be mixed with purified dry air; via cyclone separator, entering into the airflow breaker of fluid bed to be broken and classified; then the fine powder is collected in the collector to generate dry politef powder. The inventnion can continuously and automatically supply politef powder at high quality, in sealed tube.
Description
Technical field
The present invention relates to the job operation of polymeric material and be used for this job operation and contain the equipment of special delivery nozzles.Specifically, the present invention relates to the equipment that a kind of polytetrafluoroethylgranule granule that suspension polymerization is made is processed into the compact grained method, is applicable to the delivery nozzles of this method and is used to process this polytetrafluoroethylfine fine particle and contains described delivery nozzles.
Background technology
Polytetrafluoroethylene (being called for short PTFE) is the fabulous material of a kind of performance, and it can be ageing-resistant, and good chemical inertness is arranged, excellent electrical insulating property and good lubrication, and the serviceability temperature scope is wide, by the every profession and trade widespread use.
Polytetrafluoroethylene is a kind of thermoplastic polymer that contains long carbochain, can make by suspension polymerization.The polytetrafluoroethylene that makes with suspension method is mainly used in by compression forming or plunger extrusion forming manufacturing goods.
The particle diameter of the polytetrafluoroethylene that makes with suspension method has very big influence to the performance of the product that is processed to form with it.According to the size of particle diameter, grain polytetrafluoroethylene product and particulate polytetrafluoroethylene product during the polytetrafluoroethylene that suspension method makes can be divided into.The mean grain size of middle grain polytetrafluoroethylene is 100～300 μ m, and the mean grain size of particulate polytetrafluoroethylene is 15～50 μ m.Compare with middle grain polytetrafluoroethylene, the performance of the goods that the particulate polytetrafluoroethylene makes is more good, and the processed and applied scope is more extensive.Therefore, fitness for purpose is made the particulate polytetrafluoroethylene with the polytetrafluoroethylene that suspension method forms in some purposes.
In addition, for the particulate polytetrafluoroethylene, parameters such as the particle diameter of particulate polytetrafluoroethylene, particle size distribution, cleanliness level can greatly influence the performance of goods, are very important therefore.The particle diameter of known polytetrafluoroethylgranule granule is more little, and the pore-solids ratio of the goods that make with this polytetrafluoroethylene is just low more, and the goods internal performance is also just high more.
In order to make the particulate polytetrafluoroethylene, the Chinese patent CN1178542A of Daikin Co., Ltd. discloses a kind of manufacture method of polytetrafluoroethylmoulding moulding powder, and this method comprises the steps:
(a) tetrafluoroethylene that mechanical coarse crushing suspension polymerization obtains under the moisture state coarse particle that dewaters;
(b) sieve, wash, dewater;
(c) product that the high speed machine micro mist is broken obtains after dewatering;
(d) wash once more, separate, drying, obtain the fine polytetrafluoroethylpowder powder end.
Though this method can obtain the particulate polytetrafluoroethylene, it only is suitable for wet granulation.The disadvantage of this method is wet fine polytetrafluoroethylpowder powder to be carried out dry step be difficult to carry out continuously fast, perhaps needs very long dry channel in manufacturing equipment, thereby has improved the investment to production site and equipment, and then influence cost of product.
The U.S. Pat 4 of Germany Hoechst A-G company, 439,385 disclose a kind of in liquid medium the continuous coagulation method of polytetrafluorethylepowder powder, it comprises that the polytetrafluoroethylene that suspension polymerization is obtained adds three grades of series connected mixing plants continuously, condense into powder through stirring to pulverize, its powder reclaims from liquid-solid mixture continuously, and liquid is separated, obtains final polytetrafluoroethylene product.But this method complex process, equipment requires high.
The method at present domestic production fine polytetrafluoroethylpowder powder end commonly used as shown in Figure 1, it is a kind of two sections job operation, i.e. grain polytetrafluorethylepowder powder in first processing sections is made the polytetrafluoroethylene of polymerization reaction kettle discharging earlier is reprocessed into the particulate polytetrafluorethylepowder powder at second processing sections with the middle grain polytetrafluorethylepowder powder of first processing sections subsequently.
The method of grain polytetrafluorethylepowder powder mainly comprises and smashs step and pneumatic conveying drying step to pieces in forming in first processing sections; The method that second processing sections forms the particulate product mainly comprises the air-flow pulverising step.
That is to say, being sent to special use after the method for grain polytetrafluorethylepowder powder comprises polytetrafluoroethylene coarse particle that suspension polymerization is directly obtained and deionized water evenly mixes in the described formation continuously smashs to pieces and smashs to pieces in the device and wash, form the wet granular (promptly smashing step to pieces) that purifies, by regulating the rotating speed that described special use smashs the spiral separation auger in the device to pieces material and moisture are strengthened mass transfer from exporting to have in the dryer that purifies hot air again, conduct heat, and then carry out gas solid separation by cyclone, described drying and separating step (being the pneumatic conveying drying step) can repeat one or many, and generating dry mean grain size is the middle grain polytetrafluorethylepowder powder of 100-300 μ m.Thisly smash the Chinese patent 97125206.8 that is entitled as " the continuous preparation technology and the equipment thereof of suspension method polytetrafluorethylepowder powder " that step and air-flow drying method can for example be submitted to referring on December 29th, 1997 to pieces.
The desciccate of cyclone discharging (promptly by) has the powder of gaseous suspension because the middle grain polytetrafluorethylepowder powder finished product that the first processing sections pneumatic conveying drying step finally makes, therefore be difficult to it is directly sent into dosing unit, otherwise can stop up the nozzle of dosing unit.Therefore, grain polytetrafluorethylepowder powder finished product packing during prior art has to earlier it is precipitated as further is processed into the particulate product subsequently again in the following process section.But in case grain polytetrafluorethylepowder powder finished product packing in being precipitated as, this mean grain size only can be reunited, lump for the middle grain polytetrafluorethylepowder powder of 100-300 μ m.
In order to obtain the particulate product, at second processing sections middle grain polytetrafluorethylepowder powder that first processing sections makes is manually added uncovered dosing unit, enter the loose machine of smashing again, in group, the piece of grain material send into the horizontal gas flow comminutor after smashing, fine powder after the pulverizing is collected at drip catcher, generates dry fine polytetrafluoroethylpowder powder end.
Though existing method can make the particulate polytetrafluorethylepowder powder, there are many shortcomings in it, for example:
1. owing to do not find the suitable technique means that connect two processing sections, therefore prior art have between two processing sections, to adopt artificial intermittently reinforced in the operation of a polytetrafluorethylepowder powder, cause particle diameter only for the powder material contaminated environment of 100-300 micron, this operation labour intensity is big, and material loss is many;
2. the product produced of prior art, particle size distribution is wide, and particle diameter is bigger, influences the goods internal performance, and field of application is restricted;
3. the product produced of prior art, it is low to pulverize usefulness, the product energy consumption height;
4. owing to adopt two-stage method to process, first section finished product can lump, reunite.Therefore in the time of second section, the finished product of caking, reunion need be pulverized again again.Such duplication of labour has improved the cost of product, has increased energy consumption, has reduced capacity rating.
Therefore, need a kind of polytetrafluoroethylgranule granule that in a processing sections, continuously suspension polymerization is made of exploitation to be processed into the method for particulate polytetrafluoroethylene.This method has pulverizes usefulness height, advantage that product energy consumption is low, and the polytetrafluoroethylene particle size distribution that makes is in this way concentrated, adjustable grain.
Also need to develop the equipment that a kind of polytetrafluoroethylgranule granule that continuously suspension polymerization is made is processed into the particulate polytetrafluoroethylene in a processing sections.
Summary of the invention
Purpose of the present invention is to overcome prior art to have defective, provides a kind of polytetrafluoroethylgranule granule that continuously suspension polymerization is made in a processing sections to be processed into the method for particulate polytetrafluoroethylene.This method has the usefulness of pulverizing height, low, the degree of automation advantages of higher of product energy consumption, and the polytetrafluoroethylene particle size distribution that makes is in this way concentrated, adjustable grain.
Another object of the present invention provides the equipment that a kind of polytetrafluoroethylgranule granule that continuously suspension polymerization is made is processed into the particulate polytetrafluoroethylene in a processing sections.
Above-mentioned purpose of the present invention can be achieved through the following technical solutions:
One aspect of the present invention provides a kind of delivery nozzles, and it comprises:
Jet pipe (1) as the delivery nozzles inlet point;
Middle grain material inlet pipe (6), it links to each other in the L-shaped vertical fluid in the exit of this jet pipe with described jet pipe (1);
Baffle plate (2), the axis that it is arranged in described grain material inlet pipe (6) and described material inlet pipe is 20-40.Angle;
Collapsible tube (3), it links to each other with described middle grain material inlet pipe (a 6) fluid with described jet pipe (1), and the three is ⊥ shape;
Enlarged tube (4), it links to each other with carrying collapsible tube (3) fluid;
Described jet pipe (1) flare is narrowed down gradually by dry air inlet point to dry air discharging opening, and the bore of its dry air discharging opening is d1;
Described collapsible tube (3) is by big diminishing tubaeform, and the outlet bore is d2;
Described collapsible tube outlet bore d2 and the ratio d2/d1 of described jet pipe outlet bore d1 are 1.5～2.8;
Described baffle plate (2) bottom is 15～20mm to the frontier distance (s) of the gaseous blast of jet pipe (1) ejection.
In a better example of the present invention, it also comprises one or more side dry air entrance pipes (5) that described enlarged tube is communicated with extraneous fluid in described delivery nozzles sidewall, and this side dry air entrance pipe (5) leans forward along the axis of described enlarged tube.
In another better example of the present invention, the discharging opening of described jet pipe has straight-run of pipe, be used for the stable dry air stream that partly quickens through tubaeform jet pipe, the straight tube outlet of this jet pipe is no more than and baffle plate (2) plane that the axis of grain material inlet pipe (6) forms in described of intersecting, top down.
In another better example of the present invention, described baffle plate (2) is circular arc, and the inlet calibre R of described middle grain material inlet pipe (6) is 3 with the ratio of outlet bore r: 1-2.
One aspect of the present invention provides a kind of polytetrafluoroethylgranule granule that suspension polymerization is made to be processed into the method for fine grained powder, it comprises that the polytetrafluoroethylene coarse particle that suspension reaction is made smashs to pieces, the step of grain polytetrafluorethylepowder powder in the formation is characterized in that it also comprises:
(1) with windstream grain polytetrafluorethylepowder powder in described is attracted/pushes to enter fluidized bed air flow crusher by above-mentioned delivery nozzles;
(2) pulverize above-mentioned middle grain polytetrafluorethylepowder powder with fluidized bed air flow crusher; With
(3) collect the particulate polytetrafluorethylepowder powder of pulverizing through fluidized bed air flow crusher.
Another aspect of the present invention provides a kind of equipment that is used to implement described job operation, and this equipment comprises:
Smash device to pieces, the polytetrafluoroethylene coarse particle that is used for suspension reaction is made is smashed to pieces, grain polytetrafluorethylepowder powder in the formation;
It is characterized in that described equipment also comprises:
(1) smashs the delivery nozzles of the present invention that device links to each other to pieces with described, so that the described middle grain polytetrafluorethylepowder powder of smashing device formation to pieces is entered fluidized bed air flow crusher by this delivery nozzles attraction/propelling movement with windstream;
(2) fluidized bed air flow crusher that links to each other with described delivery nozzles; Be used for pulverizing the grain polytetrafluoroethylgranule granule of smashing device formation to pieces;
(3) drip catcher that links to each other with this fluidized bed air flow crusher is used to collect the particulate polytetrafluorethylepowder powder of pulverizing through fluidized bed air flow crusher.
Description of drawings
Illustrate in greater detail the present invention below in conjunction with accompanying drawing.In the accompanying drawing:
Fig. 1 is a prior art particulate polytetrafluorethylepowder powder preparation technology diagram of circuit;
Fig. 2 is the particulate polytetrafluorethylepowder powder preparation technology diagram of circuit of a better example of the present invention;
Fig. 3 is the scheme drawing of the delivery nozzles of a better example use of the present invention.
The specific embodiment
In the present invention, term " axis along enlarged tube leans forward " is meant that the dry air in the delivery nozzles sprays into center shaft and acute angle of axes intersect formation of pipeline (being side dry air entrance pipe (5)), this acute angle is preferably 20-40 °, more preferably 25-35 °, is preferably 30 °.
Term " middle grain polytetrafluoroethylene " is meant that mean grain size is 100～300 μ m, is preferably the polytetrafluoroethylgranule granule that the suspension method of 150-250 μ m through pulverizing makes.
Term " particulate polytetrafluoroethylene " is meant that mean grain size is 15～50 μ m, is preferably the polytetrafluoroethylgranule granule that the suspension method of 25-35 μ m makes.
Term " with the following plane that the axis of grain material inlet pipe (6) forms in described of intersecting, top of baffle plate (2) " is meant such plane, the parallel axes of it and middle grain material inlet pipe (6), with the axis normal of described enlarged tube (4), and the bottom of this plane and described baffle plate (following endvertex) is crossing.
One aspect of the present invention provides a kind of polytetrafluoroethylgranule granule that suspension polymerization is made to be processed into the method for fine grained powder, and it comprises with smashing device to pieces smashs the polytetrafluoroethylene coarse particle that suspension reaction makes to pieces, the step of grain polytetrafluorethylepowder powder in the formation.
Be used for the inventive method form in the grain polytetrafluoroethylene smash the device of smashing to pieces that device can be any routine to pieces.
For example, Chinese patent 97125205.x (document is inserted this paper by reference as a part of the present invention) discloses the device of smashing to pieces of a kind of suspension method teflon resin special use, it comprises smashs bucket, mixer and spiral separation auger to pieces, described mixer and spiral separation auger are by driving device drive work, the described bucket of smashing to pieces comprises staving and bucket cover: described staving is provided with cooling jacket outward, correspondence is provided with at least two toothed baffle plates in the staving, a sheathed filter in the coolant outlet pipe of staving bottom; Described bucket cover covers by middle barrel that links to each other and goes up the bucket cover and constitutes, and is located at the top of staving, and described middle barrel of cover is provided with inlet point and visor; Described mixer is installed in staving at interior the end, and this mixer is three layers, and the upper strata is a propeller blade, and the middle level is a shear blade, and lower floor is centrifugal slurry; Described stirrer shaft envelope adopts the relative rotary connection with the tetrafluoro seat of tetrafluoro radiation fins.The leading portion of described spiral separation auger is stretched in last bucket cover, and it is 10 °-30 ° horizontal by an angle that leans forward, and is preferably 20 °.
In a better example of the present invention, the described step of smashing to pieces is following carrying out, and promptly opens the baiting valve of polymerization reaction kettle, and the polytetrafluoroethylene material that suspension polymerization is made enters by vomit pipe smashs device to pieces.Add appropriate amount of deionized water after removing the polymerization reaction mother liquor with lift pump, start the puddle mixer of smashing device to pieces subsequently and smash to pieces, wash.
In smashing process to pieces, need to make material pH value reach 6～7 with the polymerization reaction auxiliary agent in the deionized water flush away material, washing times is many more, and clean result is good more, but the deionized water consumption is big, and the deionized water consumption directly influences cost of product.After having read content disclosed by the invention, those of ordinary skill in the art can easily determine suitable washing times according to its expertise, thereby has both reached the purpose of washing fully, saves deionized water again.
In a better example of the present invention, washing times is set at 5-6 time, can meet the requirement of pH value.
Deionized water conductivity after the inventive method requires to smash to pieces, wash is less than 4.0 μ s/cm, and material particular diameter (particle diameter of promptly wet middle grain polytetrafluorethylepowder powder aggregate) is 0.05～0.20 millimeter.The temperature of smashing to pieces, washing is controlled at 2 ℃～20 ℃.
After smashing step to pieces and finishing, also can carry out drying, so that make this aggregate can easily be dispersed into discrete middle grain polytetrafluorethylepowder powder to the middle grain polytetrafluoroethylgranule granule aggregate that forms.Before dry materials, can implement dehydration to improve dry efficient.In a better example of the present invention, in order to reduce the water ratio that enters the dryer section material, the elongated cylindrical material formula spiral separation auger that inclines is leaned forward to be installed in and smashs the bucket top to pieces, the material that promotes water entrainment moves forward.Because of inclining the material effect, make the aqueous reflux of carrying secretly in the material advance to smash to pieces in the bucket, reach the purpose of separation, convey materials.
Described spiral separation auger can be selected the variable pitch formula for use.Along with material moves forward, pitch increases gradually, makes material keep loose, prevents that the material caking from entering feeder, blocking pipe.
In a better example of the present invention, carry with the spiral separation auger through pulverize and the middle grain polytetrafluoroethylene wet granular of washing in the process of subsequent handling, can in smashing device to pieces, add proper amount of deionized water again, make it keep certain discharging liquid level, optimal liquid level is for smashing the nadir that device contacts at the spiral separation auger to pieces with special use.The rotating speed of control spiral separation auger when output is controlled at by 20 rev/mins and progressively rises to 200 rev/mins.Make material and moisture from after, evenly be delivered to subsequent process steps.
From smash to pieces the device discharging the grain polytetrafluoroethylene be moist cluster of grains aggressiveness or particulate mass.The aggregate of this humidity is unfavorable for that automation transmits or further pulverizes processing.Therefore, in order to improve crush efficiency, can dehydrate this moist aggregate.Those having ordinary skill in the art will appreciate that the described method that dehydrates is without particular limitation, pulverize processed powders as long as the middle grain material of agglomerated is formed with to be beneficial to.
In an example of the present invention, to implementing the heat drying step from the wet aggregate of grain polytetrafluoroethylene through washing of smashing the device discharging to pieces.For example can will send into a nozzle by screw feeder through the middle grain material aggregate of smashing to pieces, simultaneously with the middle grain material aggregate in the high temperature compressed air attraction nozzle that purifies, the negative pressure of utilizing described high temperature compressed air through purifying to produce in nozzle will be mixed with the material of air and send into a cyclone dryer heating through nozzle, send into the air separation that cyclone (below be called the 1# cyclone) makes material and water content again, obtain material through anh heat, thus the reunion degree of grain material and/or form discrete middle grain polytetrafluorethylepowder powder in the polytetrafluoroethylene that reduces to wet.
The screw feeder, feed introduction, cyclone dryer and the cyclone that are applicable to the inventive method are without particular limitation, and they can be this area screw feeder, feed introduction, cyclone dryer and cyclones commonly used.For example, described screw feeder can be a LX type screw feeder, available from Shanghai Sanaifu New Material Co., Ltd; Described feed introduction can be a PZ type feed introduction, available from Shanghai Sanaifu New Material Co., Ltd; Described cyclone dryer can be an XGS type cyclone dryer, available from Shanghai Sanaifu New Material Co., Ltd; Described cyclone can be a FL type cyclone, available from Shanghai Sanaifu New Material Co., Ltd.
In order further to remove moisture to improve crush efficiency, the thermal material of this drying is mixed once more with the normal temperature compressed air of purification, and use a cyclone (below be called the 2# cyclone) to carry out gas-solid separation once more, utilize normal temperature compressed air carrying band to remove moisture in the thermal material, reach the purpose of further drying.That is to say,, and in this cold wind nozzle, feed normal temperature compressed air middle grain polytetrafluoroethylene discharging to a nozzle of the heat of 1# cyclone discharging (below be referred to as the cold wind nozzle).Utilize pressurized air to remove moisture in the middle grain polytetrafluoroethylene of described heat, and utilize this compressed-air actuated thrust that a described middle polytetrafluoroethylene is sent into the 2# cyclone, further remove moisture after the gas-solid separation.
Can adopt the cyclone identical as the 2# cyclone with described 1# cyclone, described cold wind structure of nozzle also can be identical with the structure of the feed introduction of using previously, for example, they all can be available from Shanghai Sanaifu New Material Co., Ltd.
The method of grain polytetrafluoroethylene can be for example referring to Chinese patent 97125206.8 in being used to form, and the document is inserted this paper by reference as a part of the present invention.
One of improvements over the prior art of the present invention are with windstream a described middle grain polytetrafluorethylepowder powder that makes previously to be attracted/push to enter fluidized bed air flow crusher by delivery nozzles of the present invention.
As shown in Figure 3, be applicable to that delivery nozzles of the present invention is made up of jet pipe 1, baffle plate 2, collapsible tube 3, enlarged tube 4, middle grain material inlet pipe 6 and side dry air entrance pipe 5.
The dry air that is used for this delivery nozzles can be purifying air of the drying that makes through dehumidifier or with other method.
A middle grain material inlet pipe 6 links to each other in the L-shaped vertical fluid in the exit of this jet pipe with described jet pipe 1.A grain material inlet pipe 6 can be a cylindrical pipeline always in described, and the centre has baffle plate 2.
The axis that baffle plate 2 is arranged in described grain material inlet pipe 6 and described material inlet pipe is 20-40 ° angle.This angle is preferably 25-35 °, more preferably 28-30 °.The dry air of certain flow can produce the dry air stream that a flare enlarges gradually when the exit portion (or straight-tube portion of jet pipe 1) from jet pipe 1 penetrates.The length of baffle plate 2 should make this baffle plate following top and this tubaeform air-flow the border be 15～20mm apart from s, be preferably 17-19mm.
The length of described baffle plate 2 can be regulated according to the flow and the pressure of the dry air that enters jet pipe 1.In a better example of the present invention, the birds-eye view of baffle plate 2 (promptly look down from the top of Fig. 3 or along described grain material inlet pipe 6 radially) is circular arc, described in the ratio of inlet calibre R (this inlet calibre R is the length of perpendicular of top circular arc and middle grain material inlet pipe 6 circular arc intersection point lines on the baffle plate 2) and outlet bore r (outlet bore r correspondingly is the length of perpendicular of 2 times top circular arcs of baffle plate and middle grain material inlet pipe 6 circular arc intersection point lines) of grain material inlet pipe 6 be 3: 1-2.
When describing nozzle of the present invention, term " the last top of baffle plate 2 " is meant, in the nozzle as shown in Figure 3, with described in grain material inlet pipe 6 the entrance or enter the mouth near baffle plate 2 tops that link to each other;
Correspondingly term " the following top of baffle plate 2 " is meant, in the nozzle as shown in Figure 3, with described near link to each other the exit of grain material inlet pipe 6 or the outlet baffle plate 2 tops.
By top description as seen, the bore of grain material inlet pipe was diminished gradually by the direction of entrance to jet pipe 1 during baffle plate 2 of the present invention made.The effect of baffle plate 2 in nozzle of the present invention is to utilize the variation of sectional area to make under the situation of constant flow to enter the middle grain material acceleration of nozzle, thereby avoids middle grain material inlet pipe plug plug.
The outlet bore of this collapsible tube is d2, and the ratio d2/d1 of described collapsible tube outlet bore d2 and described jet pipe outlet bore d1 is 1.5～2.8, is preferably 1.9～2.4, more preferably 2.0～2.3.
In the present invention, term " widening angle of enlarged tube 4 " is meant in the diverging duct section, and the angle between the axisymmetric dual-side in center.Because material can reduce flow velocity after becoming in the big enlarged tube gradually gradually entering bore, therefore in a better example of the present invention, in described delivery nozzles sidewall, increase one or more side dry air entrance pipes 5 that described enlarged tube small-caliber end is communicated with extraneous fluid as shown in Figure 3, be used to spray into high-speed air flow, with the flow velocity of logistics in the quickening enlarged tube, thereby improve flow.Therefore, this side dry air entrance pipe 5 leans forward along the axis of described enlarged tube; Promptly the center shaft of this side dry air entrance pipe 5 and enlarged tube center shaft intersect acute angle of formation, and this acute angle is preferably 20-40 °, more preferably 25-35 °, is preferably 30 °.
During operation, dry air produces high speed jet stream by jet pipe 1, injection orifice at middle grain material inlet pipe 6 bottom narrow parts produces local depression, attracts the air-flow of upper class device (for example 2# cyclone) and middle grain material to enter delivery nozzles by middle grain material inlet pipe 6.The middle grain material that enters grain material inlet pipe 6 quickens under the effect of baffle plate 2, and enters collapsible tube 3 under the promotion of dry air.Middle grain material is subjected to from the impact and the dispersion of the gaseous blast of jet pipe 1 ejection, thereby avoids the intersection of the jet pipe 1 ⊥ shape, middle grain material inlet pipe 6 and collapsible tube 3 to reunite, precipitate.
After quickening, the air-flow that enters grain material powder in the containing of collapsible tube 3 enters enlarged tube 4 in collapsible tube.The air-flow that enters containing of enlarged tube 4 of middle grain powder is subjected to the effect of the gaseous blast of side dry air entrance pipe 5 ejections at the small-bore place of enlarged tube, thereby impacted, disperseed and quickened, thereby after further mixing, boost, the dry air that the middle grain material of dispersion and dry air entrance pipe 5 are from the side sprayed is transported to the next stage processing unit (plant), for example fluidized bed air flow crusher.The dry air of dry air entrance pipe 5 ejection from the side also help to prevent described in a grain material reunite, deposit, make it to keep the pulverulence that disperses.
Delivery nozzles of the present invention is characterised in that:
(a) the middle grain material inlet pipe at delivery nozzles is provided with baffle plate 2, and the feeding-passage of grain material dwindles gradually in making, thereby but the middle grain material of gentle acceleration input prevents that it from reuniting, deposition in middle grain material inlet pipe, stop up delivery nozzles;
(b) baffle plate 2 bottoms are 15～20mm to the frontier distance s of the gaseous blast of jet pipe 1 outlet ejection, and the high velocity air that helps the jet pipe ejection impacts, disperses the middle grain material that enters nozzle, prevents its reunion, deposition;
(c) jet pipe is gone out bore d1 and collapsible tube and go out bore d2 to be set at d2/d1 be 1.5～2.8, can unimpededly enter the next stage delivery duct through this delivery nozzles to guarantee the middle grain material that enters delivery nozzles; And
(d) side dry air entrance pipe 5 is set at the small-bore place of enlarged tube, from the high-speed air flow of this side dry air entrance pipe 5 ejections help to enter enlarged tube a grain material impact, disperse and quickens, make it to be difficult to reunion in enlarged tube, deposit.
Suction/thrust that delivery nozzles of the present invention utilizes dry air to produce imports next stage processing unit (plant) (for example fluidized bed air flow crusher) with middle grain material by upper class processing unit (plant) (for example 2# cyclone), need manually refute the defective that connects thereby overcome prior art, reach the purpose of automated production.
For contained moisture in the grain polytetrafluorethylepowder powder in further removing, improve the crush efficiency of fluidized bed air flow crusher, also can between described delivery nozzles and fluidized bed air flow crusher, set up a cyclone (below be called the 3# cyclone).
In a better example of the present invention, use through purify, after the normal temperature air of dehumidifying enters the 3# cyclone by delivery nozzles attraction/propelling movement and further dewaters, a middle grain material is crossed a butterfly valve with air communication and is entered fluidized bed air flow crusher, particle after the pulverizing is by the grading wheel classification, continue in the coarse particle return cavity to pulverize, fine grained enters drip catcher with air-flow and collects, and generates the fine polytetrafluoroethylpowder powder end, and the air after the separation is by blower fan emptying.
The dish valve that is applicable to the inventive method is without particular limitation, can be this area dish valve commonly used.
In a better example of the present invention, described 3
#The pressure of cyclone is 8.7～14.5KPa, is preferably 10.1-13.2kPa; The fluidized bed air flow crusher chamber pressure is 7.5～12.5KPa, is preferably 9.8-11.5kPa; Cyclone and fluidized bed air flow crusher chamber pressure difference are 1.2～2.5KPa, are preferably 1.8-2.2kPa; It is 20～60 times/minute that butterfly valve opens and closes frequency.
In a better example of the present invention, the air pressure that enters fluidized bed airflow powder machine is 0.5～1.0MPa, and temperature is 5～18 ℃, and water ratio is 0.23～0.52g/m
3, the air water ratio that enters delivery nozzles is 0.076～0.14g/m
3
In operation during fluidized bed air flow crusher,, make that material keeps certain material level in the fluidized bed air flow crusher chamber in order to obtain best crush efficiency.When material level arrives higher limit, stop screw feeder; When material level during in lower limit, open screw feeder, the screw feeder rotating speed is 6～25 rev/mins.
In above-mentioned control fluidized bed air flow crusher chamber, in the operation of level of filler material, after described screw feeder shut down 10～20 minutes, stop pressurized air and advance fluidized bed air flow crusher, and compressor is unloaded automatically; After the screw feeder running, open pressurized air and enter airslide disintegrating mill, and make the compressor heavy duty.
The best crush efficiency of concrete fluidized bed air flow crusher is depended in the setting of level of filler material in the described fluidized bed air flow crusher chamber.In general, set this material level according to the weight principle.Those of ordinary skill in the art can easily set suitable material level higher limit and lower limit after having read content disclosed by the invention and according to the concrete fluidized bed air flow crusher that adopts.
In a better example of the present invention, in described 3# cyclone lower cone exit a divergent nozzle is set, the divergent nozzle pressure source is that 0.2～0.5MPa purifies dry air, injection frequency is 1～15 time/minute.
The 3# cyclone that is applicable to the inventive method can be the identical cyclone of cyclone that uses with preceding step.In addition, fluidized bed air flow crusher and the fine grained drip catcher that is used for pulverizing the grain material can be this area fluidized bed air flow crusher and fine grained drip catcher commonly used.For example, described fluidized bed air flow crusher can be the fluidized bed air flow crusher of LQF type available from Shanghai Sanaifu New Material Co., Ltd; Described fine grained drip catcher can be the fine grained drip catcher of AEM type available from Shanghai Sanaifu New Material Co., Ltd.
In a better example of the present invention, described drip catcher is a plurality of filter bags, and the inside of filter bag to form negative pressure, enters this drip catcher thereby help trickle particulate polytetrafluoroethylene with the blower fan pump drainage.
Fig. 2 is the particulate polytetrafluorethylepowder powder preparation technology diagram of circuit of a better example of the present invention.As shown in Figure 2, the present invention's better equipment of being used for the polytetrafluoroethylgranule granule that suspension polymerization makes is processed into fine grained powder comprises successively:
(a) smash device to pieces, the polytetrafluoroethylene coarse particle that is used for suspension reaction is made is smashed to pieces, grain polytetrafluorethylepowder powder in the formation;
(b) smash the delivery nozzles of the present invention that device links to each other to pieces with described, so that the described middle grain polytetrafluorethylepowder powder of smashing device formation to pieces is entered fluidized bed air flow crusher by this delivery nozzles attraction/propelling movement with windstream;
(c) fluidized bed air flow crusher that links to each other with described delivery nozzles is used for pulverizing the grain polytetrafluoroethylgranule granule of smashing device formation to pieces; With
(d) drip catcher that links to each other with this fluidized bed air flow crusher is used to collect the particulate polytetrafluorethylepowder powder of pulverizing through fluidized bed air flow crusher.
In order to improve crush efficiency, prevent from delivery nozzles of the present invention is delivered to the process of fluidized bed air flow crusher, to be deposited in the delivery duct at the middle grain polytetrafluorethylepowder powder that will smash to pieces, in a better example of the present invention, smash described that present device also can comprise one or more levels drying and dehydrating device between device and the delivery nozzles of the present invention to pieces.
In a better example of the present invention, described drying and dehydrating device comprises:
(1) smashs the screw feeder that device links to each other to pieces with described;
(2) cyclone dryer that links to each other with described screw feeder and cyclone (1# cyclone).
In another better example of the present invention, described drying and dehydrating device comprises two-stage drying and dehydrating device, and it comprises:
(1) smashs the screw feeder that device links to each other to pieces with described;
(2) cyclone dryer that links to each other with described screw feeder and cyclone (1# cyclone);
(3) the cold wind nozzle that links to each other with described 1# cyclone;
(4) the 2# cyclone that links to each other with described cold wind nozzle;
In order to improve the crush efficiency of fluidized bed air flow crusher, after delivery nozzles discharging of the present invention but before entering described fluidized bed air flow crusher, present device also can comprise the further anh device of centering grain material.At one preferably in the example of the present invention, described equipment also comprises:
The cyclone (3# cyclone) that links to each other with described delivery nozzles fluid.
In a better example of the present invention, being used to collect fine grain drip catcher is a plurality of filter bags.The present invention another preferably in the example, in order to improve collection efficiency, also can connect blower fan on the described drip catcher so that in this drip catcher, form negative pressure.
During operation, smash the polytetrafluoroethylene adding that suspension polymerization makes to pieces device, this is smashed device to pieces and smashs this polytetrafluoroethylene material to pieces middle grain polytetrafluoroethylgranule granule wet aggregate, with after screw feeder it is delivered in the cyclone dryer dry, dried in a grain polytetrafluoroethylene material in the 1# cyclone, dewater and forms the discrete polytetrafluorethylepowder powder of drying.
In the present invention, term " discrete powder " has opposite implication with aggregate, refers to the powder of non-aggregating state.
The also optional cold wind nozzle of the anh polytetrafluorethylepowder powder of this drying enters the 2# cyclone and further dewaters under the drive that purifies air.
The grain powder enters optional 3# cyclone dehydration through delivery nozzles of the present invention in the anh discrete polytetrafluoroethylene of described drying under the drive that purifies air.A further dehydration of process or not anh discrete middle polytetrafluorethylepowder powder are admitted in the fluidized bed air flow crusher through delivery duct to be pulverized, subsequently the particulate polytetrafluorethylepowder powder that obtains through pulverizing with the drip catcher collection.
The present invention can prepare suspension method fine polytetrafluoroethylpowder powder end continuously owing to adopted above technical scheme, and compared with prior art, the present invention has the following advantages:
1, during the present invention can make the grain polytetrafluoroethylene continuous, airtight, enter airslide disintegrating mill automatically, alleviated labour intensity, improved the product cleanliness level, reduce material loss.
2, the product particle of the present invention's production is even, and particle diameter can be regulated by purposes, and the goods internal performance is good, applied range.
3, the present invention makes pulverizing process be connected with drying process, has the best usefulness of pulverizing, and the energy consumption of producing fine polytetrafluoroethylpowder powder per ton end compared with prior art descends 80%.
In a word, the present invention can be under the pipeline air-tight state long-time continuous, prepare the fine polytetrafluoroethylpowder powder end automatically, good quality of product, uniform particles, particle diameter is regulated arbitrarily in the 5-80 mu m range; Product water ratio low (water ratio≤0.01%), bulk density is 330-460g/l; With the goods applied range that particulate polytetrafluoroethylene of the present invention makes, can prepare high-quality electrical equipment film and high strength filled articles.
Further specify the present invention with embodiment below.
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 6r/min, dry, cooling, the middle grain material mean grain size 249 μ m after separating, water ratio is 0.02%.
To purify normal temperature air by dehumidifier, water ratio is 0.09g/m
3, use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 15mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 1.9, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered 3 during 3: 1 delivery nozzles attracted
#Cyclone, middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, and it is 28 times/minute that butterfly valve opens and closes frequency, 3
#Cyclone pressure is 11.9KPa, and the fluidized bed air flow crusher cavity pressure is 10.2KPa.The air pressure of pulverizing usefulness is 0.8MPa, and temperature is 16 ℃, and water ratio is 0.42g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 15.2 μ m, and D97 directly is 50 μ m, and bulk density is 360g/l, and specific surface area is 0.838m
2/ m
3, water ratio is 0.01%.
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 10r/min, dry, cooling, the middle grain material mean grain size 212 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.12g/m
3, use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 18mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.0, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered 3 during 3: 2 delivery nozzles attracted
#Cyclone, middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, and it is 30 times/minute that butterfly valve opens and closes frequency, 3
#Cyclone pressure is 11.2KPa, and the fluidized bed air flow crusher cavity pressure is 9.6KPa.The air pressure of pulverizing usefulness is 0.6MPa, and temperature is 12 ℃, and water ratio is 0.38g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 18.9 μ m, and D97 directly is 61.8 μ m, and bulk density is 380g/l, and specific surface area is 0.685m
2/ m
3, water ratio is 0.01%.
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 18r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3, use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 17mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.3, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered 3 during 3: 1.5 delivery nozzles attracted
#Cyclone, middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, and it is 24 times/minute that butterfly valve opens and closes frequency, 3
#Cyclone pressure is 10.1KPa, and fluidized bed airflow crushing chamber internal pressure is 8.6KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 18r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3, using the baffle plate bottom is that the ratio of inlet calibre R and the outlet bore r of grain material inlet pipe 6 in 2.2 is that a grain material entered 3 during 3: 1.8 delivery nozzles attracted as the ratio d2/d1 of 18mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 to the frontier distance s of gaseous blast
#Cyclone, middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, and it is 35 times/minute that butterfly valve opens and closes frequency, 3
#Cyclone pressure is 12.5KPa, and fluidized bed airflow crushing chamber internal pressure is 10.7KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
Embodiment 5
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 16r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3Use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 18mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.1, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered the 3# cyclone during 3: 1 delivery nozzles attracted, a middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, it is 20 times/minute that butterfly valve opens and closes frequency, 3# cyclone pressure is 8.7KPa, and fluidized bed airflow crushing chamber internal pressure is 7.5KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m3, and the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
Embodiment 6
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 18r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3Use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 19mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.2, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered the 3# cyclone during 3: 1.5 delivery nozzles attracted, a middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, it is 60 times/minute that butterfly valve opens and closes frequency, 3# cyclone pressure is 14.5KPa, and fluidized bed airflow crushing chamber internal pressure is 12.2KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
Embodiment 7
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 18r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3Use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 18mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.4, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered the 3# cyclone during 3: 1.1 delivery nozzles attracted, a middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, it is 45 times/minute that butterfly valve opens and closes frequency, 3# cyclone pressure is 13.2KPa, and fluidized bed airflow crushing chamber internal pressure is 11.1KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
Embodiment 8
With the polytetrafluoroethylene coarse particle after the polymerization reaction, through after smashing to pieces, wash, separating, quantitatively send into cyclone dryer by screw feeder again, screw feeder rotating speed 18r/min, dry, cooling, the middle grain material mean grain size 284 μ m after separating, water ratio is 0.02%.
Purified normal temperature air by dehumidifier, water ratio is 0.10g/m
3, use the baffle plate bottom to the frontier distance s of gaseous blast as the ratio d2/d1 of 17mm, jet pipe outlet bore d1 and collapsible tube outlet bore d2 be 2.3, the ratio of the inlet calibre R of middle grain material inlet pipe 6 and outlet bore r is that a grain material entered 3 during 3: 1 delivery nozzles attracted
#Cyclone, middle grain material is crossed butterfly valve with air communication and is entered in the fluidized bed air flow crusher chamber, and it is 52 times/minute that butterfly valve opens and closes frequency, 3
#Cyclone pressure is 9.1KPa, and fluidized bed airflow crushing chamber internal pressure is 7.8KPa.The air pressure of pulverizing usefulness is 0.5MPa, and temperature is 15 ℃, and water ratio is 0.40g/m
3, the particle after the pulverizing continues in the coarse particle return cavity to pulverize by the grading wheel classification, and fine grained enters drip catcher with air-flow and collects.
Regulating back finished product materials mean grain size is 26.1 μ m, and D97 directly is 87 μ m, and bulk density is 400g/l, and specific surface area is 0.511m
2/ m
3, water ratio is 0.01%.
By top description as seen, the polytetrafluoroethylene that the inventor utilizes delivery nozzles of the present invention efficiently suspension polymerization to be made is made the particulate polytetrafluoroethylene, save productive costs widely, prevented the dust pollution on the environment, obtained favourable technique effect.
Claims (25)
1. delivery nozzles, it comprises:
Jet pipe (1) as dry air import in the delivery nozzles;
Middle grain material inlet pipe (6), it links to each other in the L-shaped vertical fluid in the exit of this jet pipe with described jet pipe (1);
Baffle plate (2), the axis that it is arranged in described grain material inlet pipe (6) and described material inlet pipe is 20 °-40 ° angle;
Collapsible tube (3), it links to each other with described middle grain material inlet pipe (a 6) fluid with described jet pipe (1), and the three is ⊥ shape;
Enlarged tube (4), it links to each other with described collapsible tube (3) fluid;
Described jet pipe (1) flare is narrowed down gradually by dry air import to dry air outlet, and the bore of its dry air outlet is d1;
Described collapsible tube (3) is by big diminishing tubaeform, and the outlet bore is d2;
Described collapsible tube outlet bore d2 and the ratio d2/d1 of described jet pipe outlet bore d1 are 1.5～2.8;
Described baffle plate (2) bottom is 15～20mm to the frontier distance (s) of the gaseous blast of jet pipe (1) ejection.
2. delivery nozzles as claimed in claim 1, it is characterized in that it also comprises one or more side dry air entrance pipes (5) that described enlarged tube is communicated with extraneous fluid in described delivery nozzles sidewall, this side dry air entrance pipe (5) leans forward along described enlarged tube axis.
3. delivery nozzles as claimed in claim 1 or 2, the dry air outlet that it is characterized in that described jet pipe has straight-run of pipe, be used for the stable dry air stream that partly quickens through tubaeform jet pipe, the outlet of the straight tube of this jet pipe is no more than and baffle plate (2) plane that the axis of grain material inlet pipe (6) forms in described of intersecting, top down, and this plane is perpendicular to the axis of described jet pipe (1).
4. nozzle as claimed in claim 1 or 2, it is characterized in that radially along described middle grain material inlet pipe, described baffle plate (2) is circular arc, described baffle plate (2) is gone up the length of perpendicular of top circular arc and middle grain material inlet pipe (6) circular arc intersection point line, the inlet calibre R of grain material inlet pipe (6) promptly, with the following length of perpendicular of top circular arc and middle grain material inlet pipe (6) circular arc intersection point line of baffle plate (2), promptly export bore r, ratio be 3: 1-2.
5. delivery nozzles as claimed in claim 1 or 2 is characterized in that described baffle plate bottom is 17～19mm to the frontier distance (s) of gaseous blast; And
Described collapsible tube outlet bore d2 and the ratio d2/d1 of jet pipe outlet bore d1 are 1.9～2.4.
6. the polytetrafluoroethylgranule granule that suspension polymerization is made is processed into the method for fine grained powder, it comprises that the polytetrafluoroethylene coarse particle that suspension reaction is made smashs to pieces, forming mean grain size is the step of the middle grain polytetrafluorethylepowder powder of 100-300 micron, it is characterized in that it also comprises:
(1) with windstream grain polytetrafluorethylepowder powder in described is entered fluidized bed air flow crusher by each described delivery nozzles attraction/propelling movement among the claim 1-5;
(2) collecting the mean grain size of pulverizing through fluidized bed air flow crusher is the particulate polytetrafluorethylepowder powder of 15-50 micron.
7. method as claimed in claim 6 is characterized in that the described polytetrafluoroethylene coarse particle that suspension reaction is made smashs to pieces, and the step of grain polytetrafluorethylepowder powder comprises in the formation:
(i) poly-mer of polymerization reaction kettle discharging is smashed to pieces;
(ii) use the cyclone dryer drying;
(iii) dewater with cyclone.
8. method as claimed in claim 7 is characterized in that it also comprises the middle grain polytetrafluorethylepowder powder after the cyclone dehydration is delivered to next cyclone with purifying air, and further dewaters.
9. as each described method among the claim 6-8, it is characterized in that described collection realizes with filter bag through the step of the particulate polytetrafluorethylepowder powder of fluidized bed air flow crusher pulverizing.
10. method as claimed in claim 9 is characterized in that it also is included in the described filter bag to form negative pressure.
11. method as claimed in claim 7, it is characterized in that described cyclone pressure is 8.7～14.5KPa, the fluidized bed air flow crusher chamber pressure is 7.5～12.5KPa, and cyclone and fluidized bed air flow crusher chamber pressure difference are 1.2～2.5KPa.
12. as each described method among the claim 6-8, it is characterized in that using a butterfly valve control to enter middle polytetrafluorethylepowder powder carrying fluidized bed air flow crusher, it is 20～60 times/minute that this butterfly valve opens and closes frequency.
13. method as claimed in claim 11, it is characterized in that described cyclone pressure is 10.1-13.2KPa, the fluidized bed air flow crusher chamber pressure is 9.8-11.5KPa, and cyclone and fluidized bed air flow crusher chamber pressure difference are 1.8-2.2KPa.
14. method as claimed in claim 12 is characterized in that it is 30-45 time/minute that described butterfly valve opens and closes frequency.
15. according to each described method among the claim 6-8, it is characterized in that described fluidized bed air flow crusher has air compressor, the air pressure that enters fluidized bed air flow crusher is 0.5～1.0MPa, and temperature is 5～18 ℃, and water ratio is 0.23～0.52g/m
3'.
16. as each described method among the claim 6-8, the air water ratio that it is characterized in that entering by described side dry air entrance (5) delivery nozzles is 0.076～0.14g/m
3
17. method as claimed in claim 15 is characterized in that it also comprises the material level of setting material in the described fluidized bed air flow crusher chamber according to the best crush efficiency of described fluidized bed air flow crusher, when material level arrives higher limit, stops screw feeder; When material level during in lower limit, open screw feeder, the screw feeder rotating speed is 6～25 rev/mins.
18. method according to claim 17 is characterized in that stopping pressurized air and entering fluidized bed air flow crusher after described screw feeder shut down 10～20 minutes, and compressor is unloaded automatically; After the screw feeder running, open pressurized air and enter fluidized bed air flow crusher, and make the air compressor heavy duty.
19. method according to claim 7 is characterized in that, described cyclone lower cone exit is provided with divergent nozzle, and the divergent nozzle pressure source is that 0.2～0.5Mpa purifies dry air, and injection frequency is 1～15 time/minute.
20. an equipment that is used for implementing each method of claim 6-19, it comprises:
(1) smash device to pieces, the polytetrafluoroethylene coarse particle that is used for suspension reaction is made is smashed to pieces, grain polytetrafluorethylepowder powder in the formation;
It is characterized in that described equipment also comprises:
(2) with described smash that device links to each other to pieces as each described delivery nozzles among the claim 1-5, so that smash the middle grain polytetrafluorethylepowder powder that device forms to pieces and enter fluidized bed air flow crusher described by this delivery nozzles attraction/propelling movement with windstream;
(3) fluidized bed air flow crusher that links to each other with described delivery nozzles is used for pulverizing the grain polytetrafluorethylepowder powder of smashing device formation to pieces;
(4) drip catcher that links to each other with this fluidized bed air flow crusher is used to collect the particulate polytetrafluorethylepowder powder of pulverizing through fluidized bed air flow crusher.
21. equipment as claimed in claim 20, it is characterized in that the described device of smashing to pieces comprises and smashs bucket, mixer and spiral separation auger to pieces, described mixer and spiral separation auger are by driving device drive work, the described bucket of smashing to pieces comprises staving and bucket cover: described staving is provided with cooling jacket outward, correspondence is provided with at least two toothed baffle plates in the staving, a sheathed filter in the coolant outlet pipe of staving bottom; Described bucket cover covers by middle barrel that links to each other and goes up the bucket cover and constitutes, and is located at the top of staving, and described middle barrel of cover is provided with inlet point and visor; Described mixer is installed in staving at interior the end, and this mixer is three layers, and the upper strata is a propeller blade, and the middle level is a shear blade, and lower floor is centrifugal slurry; The axle envelope of described mixer adopts the relative rotary connection with the tetrafluoro seat of tetrafluoro radiation fins, and the leading portion of described spiral separation auger is stretched in last bucket cover, and it is horizontal by 10 °～30 ° of angles that leans forward.
22., it is characterized in that smashing described that described equipment also comprises one or more levels drying and dehydrating device between device and the described delivery nozzles to pieces as claim 20 or 21 described equipment.
23. equipment as claimed in claim 22 is characterized in that described drying and dehydrating device comprises:
(a) smash the screw feeder that device links to each other to pieces with described;
(b) cyclone dryer that links to each other with described screw feeder;
(c) cyclone that links to each other with described cyclone dryer.
24. equipment as claimed in claim 22 is characterized in that described drying and dehydrating device comprises two-stage drying and dehydrating device, it comprises:
(a) smash the screw feeder that device links to each other to pieces with described;
(b) cyclone dryer and the cyclone that links to each other with described screw feeder;
(c) the cold wind nozzle that links to each other with described cyclone;
(d) another cyclone that links to each other with described cold wind nozzle.
25. as claim 20 or 21 described equipment, it is characterized in that between described delivery nozzles and fluidized bed air flow crusher, which comprises at least a cyclone separator, be used for removing the moisture in the grain polytetrafluorethylepowder powder.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610026921A CN100579879C (en) | 2006-05-26 | 2006-05-26 | Delivery spray nozzle, polytetrafluoroethylene fine particle processing method and apparatus using the spray nozzle |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610026921A CN100579879C (en) | 2006-05-26 | 2006-05-26 | Delivery spray nozzle, polytetrafluoroethylene fine particle processing method and apparatus using the spray nozzle |
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| Publication Number | Publication Date |
|---|---|
| CN1876530A CN1876530A (en) | 2006-12-13 |
| CN100579879C true CN100579879C (en) | 2010-01-13 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102374767A (en) * | 2010-08-20 | 2012-03-14 | 内蒙古奈伦农业科技股份有限公司 | Feeder used for airflow drying equipment |
| CN102700027B (en) * | 2012-05-23 | 2014-08-20 | 中昊晨光化工研究院 | Teflon drying system and application thereof |
| CN103170399B (en) * | 2013-04-03 | 2015-10-28 | 太仓金凯特种线缆有限公司 | Ultraviolet prepares the method for ultrafine PTFE powder in conjunction with carbon tetrachloride |
| CN103170401B (en) * | 2013-04-03 | 2015-11-18 | 太仓金凯特种线缆有限公司 | Ultraviolet prepares the method for ultrafine PTFE powder in conjunction with hydrogen peroxide and carbon tetrachloride |
| CN103223369B (en) * | 2013-04-03 | 2015-06-03 | 太仓金凯特种线缆有限公司 | Method of preparing PTFE micropowder by ultraviolet ray |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4666083A (en) * | 1985-11-21 | 1987-05-19 | Fluidyne Corporation | Process and apparatus for generating particulate containing fluid jets |
-
2006
- 2006-05-26 CN CN200610026921A patent/CN100579879C/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4666083A (en) * | 1985-11-21 | 1987-05-19 | Fluidyne Corporation | Process and apparatus for generating particulate containing fluid jets |
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| CN1876530A (en) | 2006-12-13 |
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