CN1405367A - Method for preparing extra high molecular polyethylene high-concentrated solution for spinning - Google Patents
Method for preparing extra high molecular polyethylene high-concentrated solution for spinning Download PDFInfo
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- CN1405367A CN1405367A CN 01123600 CN01123600A CN1405367A CN 1405367 A CN1405367 A CN 1405367A CN 01123600 CN01123600 CN 01123600 CN 01123600 A CN01123600 A CN 01123600A CN 1405367 A CN1405367 A CN 1405367A
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- 229920000573 polyethylene Polymers 0.000 title claims abstract description 28
- 238000009987 spinning Methods 0.000 title claims description 41
- 239000004698 Polyethylene Substances 0.000 title claims description 25
- -1 polyethylene Polymers 0.000 title claims description 25
- 238000000034 method Methods 0.000 title description 10
- 238000003756 stirring Methods 0.000 claims abstract description 47
- 239000000843 powder Substances 0.000 claims abstract description 24
- 239000003292 glue Substances 0.000 claims abstract description 16
- 239000002002 slurry Substances 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 8
- 239000002904 solvent Substances 0.000 claims abstract description 8
- 239000012452 mother liquor Substances 0.000 claims description 55
- 239000007788 liquid Substances 0.000 claims description 25
- 238000002360 preparation method Methods 0.000 claims description 25
- 238000004090 dissolution Methods 0.000 claims description 12
- 230000035699 permeability Effects 0.000 claims description 9
- 238000005191 phase separation Methods 0.000 claims description 9
- 230000008961 swelling Effects 0.000 claims description 9
- 230000010355 oscillation Effects 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 4
- 238000009826 distribution Methods 0.000 claims description 3
- 238000010410 dusting Methods 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 239000005662 Paraffin oil Substances 0.000 claims description 2
- 229910004116 SrO 2 Inorganic materials 0.000 claims description 2
- 239000003963 antioxidant agent Substances 0.000 claims description 2
- 230000003078 antioxidant effect Effects 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 239000002086 nanomaterial Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 239000003381 stabilizer Substances 0.000 claims description 2
- 239000004699 Ultra-high molecular weight polyethylene Substances 0.000 claims 1
- 230000002045 lasting effect Effects 0.000 claims 1
- 229920000785 ultra high molecular weight polyethylene Polymers 0.000 claims 1
- 239000000243 solution Substances 0.000 abstract description 49
- 238000004519 manufacturing process Methods 0.000 abstract description 11
- 239000000835 fiber Substances 0.000 abstract description 9
- 229920000098 polyolefin Polymers 0.000 abstract description 6
- 230000008014 freezing Effects 0.000 abstract 2
- 238000007710 freezing Methods 0.000 abstract 2
- 150000001336 alkenes Chemical class 0.000 abstract 1
- 239000010413 mother solution Substances 0.000 abstract 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 6
- 229920000642 polymer Polymers 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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Abstract
The invention refers to a method of making super-high relative molecular weight high-concentration solution used for making high-intensity high-modular magnitude polythene fiber. In the dissolving kettle, stir polythene (Mw>1.5x10 to the 6th power) powder and quantitative solvent and then raise the temperature to make mother solution A; then add quantitative A into common calefactive stirring kettle, and then add quantitative polyolefine powder or freezing colloidal particle and then said them and raise the temperature to make slurry solution B; and then add quantitative A, B and solvent-permeability olefin oil to the calefactive stirring kettle to make high-concentration filature freezing glue solution.
Description
Technical field
That the present invention relates to is the preparation method of relevant polyethylene solution, belongs to ICL D04H and D01F field, and that relate in particular to is the preparation method of extra high molecular polyethylene high-concentrated solution for spinning.
Technical background
Making superelevation average molecular weight polythene uniform solution is a complicated technology job, and it is bigger to make its difficulty of high concentration spinning frozen glue liquid.Mainly be that the production cycle is long, the cost that makes high-intensity fiber that yields poorly becomes very high.In technology in the past, in order to obtain uniform spinning solution, polymer considerable time be will be mixed stage by stage with several stirred tanks simultaneously and pre-swelling and swelling carried out, put it into a temperature again near rising temperature for dissolving in the dissolution kettle of its decomposition temperature, because solution viscosity sharply increases, easily sneak into bubble in the solution, make insoluble micel and bubble constitute inhomogeneous solution; The phenomenon that another one is difficult to overcome is, when whipping temp rise to can make the abundant swelling of polymer after, dope can stick on the puddler, produces " rod-climbing effect ", to stirring can't be carried out.In technology in the past, solve above-mentioned technological problems, common technology is to adopt long-time powerful stirring of higher temperature, because thermal degradation, the result reduces polymer molecular weight significantly, the solution ends concentration increases, the fibre strength modulus that drawing-off is produced seriously descends, end breakage rate height, production poor continuity.
General introduction of the present invention
Purpose of the present invention is exactly the shortcoming that overcomes prior art, a kind of preparation method of extra high molecular polyethylene high-concentrated solution for spinning is provided, adopt the inventive method effectively to shorten the production time, produce high concentration frozen glue liquid, increase quantum of output, reduce the treating capacity of solvent, shorten the production cycle, reduce production costs, industrialization is produced continuously, expand product use field and be significant.
The objective of the invention is to realize that the preparation method of extra high molecular polyethylene high-concentrated solution for spinning of the present invention successively prepares mother liquor A, mother liquor B, mixes stirring with mother liquor A and mother liquor B again and makes the high concentration spinning solution by following technical proposals; The preparation method of wherein said mother liquor A is, polyethylene powders and solvent are put in the supersonic oscillations container for the high osmosis paraffin oil, be made into uniform slurry at normal temperatures, its objective is and make at normal temperatures and pressures can be the evenly pre-swelling of raw material, be called " expectation of A liquid ", used polyethylene is a linear polyethylene, and its non-linear rate is less than 5%; Polyolefinic molecular weight ranges should be chosen in M
W=1.5 * 10
6To M
W=7 * 10
6Between, the particle diameter of its polyethylene powders distributes and will be the Gaussian curve distribution, and its particle size range is between 80 μ-200 μ, and the molecular weight of selected high osmosis Valelinum Liquidum is between 40-1000, and the frequency of oscillation of employed ultrasonic oscillator is 1 * 10
4-4 * 10
4Between the HZ, the weight percent concentration that the A mother liquor is expected is 0.3-2%; Input permeability Valelinum Liquidum in spiral agitator, normal pressure evenly stirs down and heats up, when temperature rises to 80-90 ℃, with sprinkler " A expects pre-liquid " sprayed into, and add polyethylene powders thereupon, vacuumize then to stir and heat up, temperature rise rate remains on 1 ℃/3-5min, vacuum guarantees at-0.04-0.06Mpa, temperature is controlled at 150-250 ℃ for well, thereafter feeding the refrigerant continuous high speed in stirred tank stirs, the purpose of high-speed stirred is to guarantee sufficient heat exchange, can be changed to the frozen glue attitude of milky white by clear state at phase separation temperature point in the solution temperature-fall period, finally make weight percent concentration and be the mother liquor A of frozen glue attitude of the abundant dissolving swelling of 0.3-2%, it is standby solution to be pumped into A liquid holding vessel before inversion point; The preparation method of described mother liquor B is to produce mother liquor B with mother liquor A, concrete mode is in the combined dissolution kettle of slurry formula, add quantitative A mother liquor earlier and carry out stirring at normal temperature, simultaneously polyethylene powders is sprayed into, the molecular weight of polyethylene powders is identical with the molecular weight of system A mother liquor.The last limit of dusting, limit vacuumizes warming while stirring, programming rate is 0.5-0.8 ℃/10 minutes, when temperature rises to 60-190 ℃, when vacuumizing stirring, be incubated 20-60 minute, vacuum guarantees at-0.04-0.06Mpa, when making mother liquor B, also can be not add polyethylene powders but adding frozen glue grain, at this moment temperature in the kettle can be no more than the solution separation temperature; The ultimate density of its mother liquor B is 25%-60%, producing of mother liquor B can divide three phases, each stage can divide by concentration, phase I concentration is at 10%-20%, and second stage concentration is at 20%-40%, and the phase III, concentration was at 40%-60%, total principle is that solution concentration is produced by gradient principle, after its solution presents clear state, promptly make slurry mother liquor B, it is standby that it is dropped to natural temperature; In a kind of preferred implementation, producing of mother liquor B can divide three phases, and each stage can divide by concentration, phase I, concentration was at 10%-20%, second stage concentration is at 20%-40%, and phase III concentration is at 40%-60%, and total principle is that solution concentration is produced by gradient principle; Its described mother liquor A and mother liquor B mix that to stir the mode of making the high concentration spinning solution be the mother liquor A that will produce with the mother liquor B that produces and permeability Valelinum Liquidum join sequentially one have heat up and the dissolution kettle of anchor formula agitating device in, its concentration ratio can be formulated into 24%-60%, the steps include: mother liquor A agitating heating under natural temperature (〉=15 ℃) normal pressure is heated up, under the state that is higher than 10 ℃ of phase separation temperatures, reduce in its viscosity, when mobile performance increases, add mother liquor B, the common stirring 15-40 minute, under keeping warm mode, evenly spray into Valelinum Liquidum, continue to stir and present transparent even attitude up to solution, its solution concentration ratio can be formulated into 12%-60%, heat-exchange system with the stirring and dissolving still injects refrigerant then, continue to be cooled to 50-70 ℃ while stirring and make spinning solution, the spinning solution of high concentration can be pumped in the twin (double) screw extruder under 50-70 ℃ of temperature subsequently.
Spinning solution is the feeding section that joins the twin-screw spinning machine, and spinning solution is heated to more than 200 ℃ at extruder screw mixer and compression section in extrusion, is spun into gel fiber through dosing pump, spinning head, water-bath setting then.
At one preferably in the embodiment, wherein of the present invention:
1. the manufacturing of mother liquor A
Superelevation average molecular weight northylen generally adopts polymer powder, generally is to adopt linear polyethylene, and its non-linear rate is less than 5%.Polyolefinic molecular weight ranges should be chosen in M
W=1.5 * 106 to M
WBetween=7 * 106.The particle diameter of its powder distributes and will be the Gaussian curve distribution, and its particle size range is between 80 μ-200 μ.Selected solvent is the high osmosis Valelinum Liquidum, and its molecular weight is between 40-1000.Equipment need adopt withstand voltage rising temperature for dissolving still, and its agitating device can adopt frame, anchor formula, slurry formula, double helix rotation revolution formula, but with the withstand voltage intensification rotation revolution of taper formula dissolution kettle for well.The revolution of its main shaft at 6-30rpm for well, the revolution of its spiral with 100-200rpm for well.During churning can add various fillers, for example SIO
2, Al
2O
3, Ag, SrO
2Etc. nano material.On the wall of taper dissolution kettle, ultrasonic oscillator is housed, the continuous in the shape of a spiral shape of its assembling mode, frequency of oscillation is 1 * 10
4-4 * 10
4Between the HZ, but 1.5 * 10
4-2.5 * 10
4Better between the HZ.Hunting power between 2KW-5KW for well.The weight percent concentration of A liquid at 0.3-2% for well, but better at 0.5-1.5%.The preparation quality of finding the A mother liquor in experiment is relevant with its solution concentration, and its concentration is relevant with the selection of solvent and raw material accurately.
At first quantitative polyolefin powder and solvent are put into the supersonic oscillations container, be made into uniform slurry at normal temperatures, its objective is to make at normal temperatures and pressures can be the evenly pre-swelling of raw material, be called " expectation of A liquid ".
The permeability Valelinum Liquidum of input predetermined weight in spiral agitator, normal pressure evenly stir down and heat up, and when temperature rises to 80-90 ℃, with sprinkler " A expects pre-liquid " are sprayed into.Vacuumize then to stir and heat up, temperature rise rate remains on 1 ℃/3-5min, and certain 1 ℃/2-3min is better.Vacuum guarantees at-0.04-0.06Mpa, stirs the revolution revolution at 50-100rpm, and rotation is at 300-500rpm.Temperature according to different Material control 150-250 ℃ for well, but serve as better with 120-220 ℃.After temperature rise puts in place, continue to stir 0.5-1 hour, be more preferably 20-30 minute.This moment, solution can be the homogeneous transparent attitude.Because temperature rise surpasses the polymer unwinds temperature, therefore to when adding material, add preferred antioxidant, stabilizing agent.Thereafter feed the refrigerant continuous high speed and stir in stirred tank, the purpose of high-speed stirred is to guarantee sufficient heat exchange, and its maximum speed can reach 2000rpm.But revolution will reduce relatively near phase separation temperature the time, and 5-10rpm is wanted in revolution, but 2-5rpm is better.
The short time of finding A liquid in experiment makes, and outside the Pass having with revolution and the time that keeps temperature, The key factor is that the continuity of cooling has the nonlinear change rule.Solution perhaps just is easy to form uniform geode attitude under the condition of cooling continuously naturally under the condition that guarantees continuous rule cooling.If using forced cooling to have accurately with regard to the heat-exchange system that requires the hot and cold matchmaker of equipment surveys, control, follow-up control.
Can change by the frozen glue attitude of clear state at phase separation temperature point in the solution temperature-fall period to milky white.We will do is that will be before inversion point solution to be pumped into A liquid holding vessel standby.
The poly phase transition temperature of its superelevation relative molecular weight is different according to the difference of molecular weight, greatly between 70-90 ℃.Precritical blowing temperature is grasped relevant with the four seasons temperature difference, and its numerical value is not subjected to the restriction of this patent.
2. the preparation of mother liquor B
In having the combined dissolution kettle of slurry formula of a whole set of intensification agitating device, add quantitative A liquid earlier and carry out stirring at normal temperature, simultaneously polyolefin powder is sprayed into, the molecular weight of polyolefin powder is identical with the molecular weight of system A liquid.The last limit of dusting, limit vacuumizes warming while stirring, and programming rate is 0.5-0.8 ℃/10 minutes, when temperature rises to 60-190 ℃, when vacuumizing stirring, is incubated 20-60 minute, certainly 20-40 minute better.The continuity of its intensification is deferred to its regularity.After this moment, solution presented clear state, it is standby that it is dropped to natural temperature.Cooling measure can be taked forced action type, also can take the method for nature cooling.If what add is the frozen glue grain, its temperature in the kettle can be no more than the phase separation temperature of solution.And the molecular weight size of the concentration of the phase separation temperature of solvent and solute and solution and solute is relevant.Generally between 60-90 ℃.Its vacuum finally remains on-0.06Mpa.Producing of B mother liquor can divide three phases, and each stage can divide by concentration.Phase I concentration is at 10%-20%, and second stage concentration is at 20%-40%, and phase III concentration is at 40%-60%, and total principle is that solution concentration is produced by gradient principle.Certainly, the thin more solution dissolving of stage division is good more, but should be principle to reduce cost, and suitably chooses concentration gradient.
Powder can be added when producing B liquid, also the frozen glue grain can be added.Because there is skin-core structure in the frozen glue grain, the particle diameter of its frozen glue is the smaller the better, and the control of temperature, pressure is analogous to above-mentioned method.In the laboratory, find to add the frozen glue grain and can obtain identical effect, just the temperature controlling difference with the adding powder.
3. spinning solution produces
With the mother liquor A that produces and mother liquor B that produces and permeability Valelinum Liquidum join sequentially one have heat up and the dissolution kettle of anchor formula agitating device in, its concentration ratio is the highest to be formulated into 60%, but the size of concentration also will be considered the quality of spinning and the ability to bear of equipment except that considering cost.Its method is as follows:
A liquid agitating heating under natural temperature (〉=15 ℃) normal pressure is heated up, under the state that is higher than 10 ℃ of phase separation temperatures, reduce in its viscosity, when mobile performance increases, add B liquid, stirred jointly 15-40 minute, its agitator revolution is high more good more under situation about allowing, evenly spray into Valelinum Liquidum under keeping warm mode, continue stirring and present transparent even attitude up to solution, its solution concentration ratio can be formulated into 12%-60%.Heat-exchange system with the stirring and dissolving still injects refrigerant then, continues to be cooled to 50-70 ℃ while stirring and makes spinning solution.
Again spinning solution is pumped into the feeding section of twin-screw spinning machine with piston pump, spinning solution is heated to more than 200 ℃ at mixer and compression section in extrusion, and then through dosing pump, spinning head, water-bath setting are spun into gel fiber.
Special what propose is that the screw slenderness ratio of twin-screw spinning machine was greater than 1: 45, to guarantee material is arranged enough time of staying in screw rod.
Gel fiber can form tensile break strength 30-35g/d, the high-tenacity polyethylene fibre of modulus 1000-1200g/d through after extracting ultra-drawing.
Splendid with the fiber continuity that said method is produced, the production cycle shortens over half than traditional handicraft.
Because the production cycle significantly shortens, the corresponding shortening of the heated time of raw material, so the thermal degradation of raw material reduces 50% than conventional art, ends concentration significantly reduces, thereby can give full play to the polyolefinic good characteristic of superelevation relative molecular weight.
Embodiment 1
Being 3,300,000 linear superelevation relative molecular weight polyolefin powder and quantitative permeability Valelinum Liquidum with molecular weight prepares 1% mother liquor A according to the method for claim 1 in the intensification stirred tank, the still temperature stirred 40 minutes in the time of 180 ℃, solution becomes clear state, emits, and is cold naturally really standby.
Prepare B liquid with identical polyethylene powder and permeability Valelinum Liquidum in three stages by the concentration of estimating.A, B liquid and quantitative Valelinum Liquidum be made into the spinning solution of 12% high concentration, the liquid temperature remain on 70 ℃ standby, pump into the feeding section of twin-screw spinning machine afterwards with piston pump, in mixer, pressurized segment temperature is raised to 300 ℃, pumping into measuring pump through force (forcing) pump again pumps spinning head and is spun into silk, 20 ℃ of water-bath setting through 40 times of drawing-offs, are stablized crook and were not had broken end around 70 hours.
Embodiment 2
Being 2,400,000 linear superelevation relative molecular weight polyolefin powder and quantitative permeability Valelinum Liquidum with molecular weight prepares 0.5% mother liquor A according to the method for claim 1 in the intensification stirred tank, the still temperature stirred 40 minutes in the time of 175 ℃, solution becomes clear state, emits, and forces cold true back standby.
Stir in stirred tank under 90 ℃ of conditions with the frozen glue grain of concentration known and Valelinum Liquidum that to be mixed with the higher slurry B liquid insulation of concentration in 30 minutes standby.A, B liquid and quantitative Valelinum Liquidum mixed to stir at normal temperatures and pressures being warmed up to 75 ℃, treat after 30 minutes that solution evenly makes the spinning solution of concentration 24%, the heat preservation for standby use of lowering the temperature afterwards.Step is produced 90 hours uninterruptedly continuously with embodiment 1 later on.
Comparative example 1
Use 2,400,000 linear polyethylene powder by conventional method in three stages at three stirred tanks with carrying out pre-swelling in 48 hours; first still was with 65 ℃ of stirrings in 24 hours; second still is with 75 ℃ of stirrings in 12 hours, and the 3rd still stirs preparation concentration with 12 hours 110 ℃, 5rpm, nitrogen protection
6% mixed solution is forced coldly really to 70 ℃, pumps into measuring pump to spinning head with piston pump and is spun into silk, method with embodiment 1,2 is carried out drawing-off, though can carry out continuous 10 hours drawing-off, fiber is inhomogeneous more serious, intensity is lower, and dissolution time is long, and production efficiency is low.
It is 1 as follows that the basic parameter of embodiment 1,2 and comparative example 1 is tabulated.
Table 1
*??*??*??*??*
| Project unit | TENSILE STRENGTH g/d | Modulus g/d | Extension at break % | Continuous reeling time hour | Matched proportion density % | Production cycle process time hour | Remarks |
| Embodiment 1 | ??30 | ??1100 | ????3 | ????60 | ????12 | ????6 | |
| Embodiment 2 | ??32 | ??1300 | ????2 | ????80 | ????24 | ????4 | |
| Comparative example 1 | ??22 | ??750 | ????4 | ????10 | ????6 | ????48 |
Claims (8)
1. the preparation method of a ultrahigh molecular weight polyethylene for spinning high concentration spinning solution is characterized in that successively preparing mother liquor A, mother liquor B, mixes to stir with mother liquor A and mother liquor B again and makes the high concentration spinning solution; The preparation method of wherein said mother liquor A is, put into polyethylene powders and solvent in the high pressure resistant rising temperature for dissolving still that the supersonic oscillations container is housed for the high osmosis paraffin oil, be made into uniform slurry at normal temperatures, its objective is and make at normal temperatures and pressures can be the evenly pre-swelling of raw material, be called " expectation of A liquid ", used polyethylene is a linear polyethylene, and its non-linear rate is less than 5%; Polyolefinic molecular weight ranges should be chosen in M
W=1.5 * 10
6To M
W=7 * 10
6Between, the particle diameter of its polyethylene powders distributes and will be the Gaussian curve distribution, and its particle size range is between 80 μ-200 μ, and the molecular weight of selected high osmosis Valelinum Liquidum is between 40-1000, and the frequency of oscillation of employed ultrasonic oscillator is 1 * 10
4-4 * 10
4Between the HZ, the weight percent concentration that A liquid is expected is 0.3-2%; Input permeability Valelinum Liquidum in spiral agitator, normal pressure evenly stirs down and heats up, when temperature rises to 80-90 ℃, with sprinkler " A expects pre-liquid " sprayed into, and add polyethylene powders thereupon, vacuumize then to stir and heat up, temperature rise rate remains on 1 ℃/3-5min, vacuum guarantees at-0.04-0.06Mpa, stir revolution revolution 50-100rpm, rotation 300-500rpm, temperature is controlled at 150-250 ℃, intensification puts in place, and the back is lasting stirred 0.2-1 hour, thereafter feed the refrigerant continuous high speed and stir in stirred tank, the purpose of high-speed stirred is to guarantee sufficient heat exchange, can be changed by the frozen glue attitude of clear state to milky white at phase separation temperature point in the solution temperature-fall period, finally make weight percent concentration and be the mother liquor A of frozen glue attitude of the abundant dissolving swelling of 0.3-2%, it is standby solution to be pumped into A liquid holding vessel before inversion point; The preparation method of described mother liquor B is to produce mother liquor B with mother liquor A, concrete mode is in the combined dissolution kettle of slurry formula, add quantitative A mother liquor earlier and carry out stirring at normal temperature, simultaneously polyethylene powders is sprayed into, the molecular weight of polyethylene powders is identical with the molecular weight of system A liquid, the last limit of dusting, limit vacuumizes warming while stirring, programming rate is 0.5-0.8 ℃/10 minutes, when temperature rises to 60-190 ℃, when vacuumizing stirring, be incubated 20-60 minute, vacuum guarantees that the ultimate density of its mother liquor B is 25%-60%, after its solution presents clear state at-0.04-0.06Mpa, promptly make slurry mother liquor B, it is standby that it is dropped to natural temperature; Its described mother liquor A and mother liquor B mix that to stir the mode of making the high concentration spinning solution be the mother liquor A that will produce with the mother liquor B that produces and permeability Valelinum Liquidum join sequentially one have heat up and the dissolution kettle of anchor formula agitating device in, its concentration ratio can be formulated into 24%-60%, the steps include: mother liquor A agitating heating under natural temperature (〉=15 ℃) normal pressure is heated up, under the state that is higher than 10 ℃ of phase separation temperatures, reduce in its viscosity, when mobile performance increases, add mother liquor B, the common stirring 15-40 minute, under keeping warm mode, evenly spray into Valelinum Liquidum, continue to stir and present transparent even attitude up to solution, its solution concentration ratio can be formulated into 12%-60%, heat-exchange system with the stirring and dissolving still injects refrigerant then, continue to be cooled to 50-70 ℃ while stirring and make spinning solution, the spinning solution of high concentration can be pumped in the twin (double) screw extruder under 50-70 ℃ of temperature subsequently.
2. the preparation method of spinning solution according to claim 1, it is characterized in that the high pressure resistant rising temperature for dissolving still that is adopted is the withstand voltage intensification rotation revolution of a taper formula dissolution kettle when preparation mother liquor A, agitating device in its dissolution kettle can adopt frame, anchor formula, slurry formula, double helix rotation revolution formula, its main shaft revolution is at 6-30rpm, the revolution of its spiral is with 100-200rpm, during churning can add various fillers, its filler is SIO
2, Al
2O
3, Ag, SrO
2Etc. nano material.
3. the preparation method of spinning solution according to claim 1 is characterized in that used supersonic oscillations frequency is 1.5 * 10 when preparation mother liquor A
4-2.5 * 10
4HZ.
4. according to the preparation method of the described spinning solution of claim 1, it is characterized in that the mother liquor A that produced concentration be 0.5-1.5%.
5. according to the preparation method of the described spinning solution of claim 1, it is characterized in that heating up when preparation mother liquor A continues can add antioxidant, stabilizing agent in the stirring.
6. according to the preparation method of the described spinning solution of claim 1, it is characterized in that its solution concentration is produced by the gradient mode when preparation mother liquor B.
7. according to the preparation method of the described spinning solution of claim 1, it is characterized in that also can adding the frozen glue grain when preparation mother liquor B, at this moment temperature in the kettle can be no more than the solution separation temperature.
8. according to the preparation method of the described spinning solution of claim 1, the screw slenderness ratio that it is characterized in that the twin (double) screw extruder that adopted was greater than 1: 45.
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| WO2005066397A1 (en) * | 2003-12-19 | 2005-07-21 | Sinotex Investment & Development Co., Ltd. | A process for preparing ultra high molecular weight polyethylene fibres |
| CN100441753C (en) * | 2006-07-18 | 2008-12-10 | 东华大学 | Prepn of hollow high-strength light-modulus polyethylene fiber |
| CN101153079B (en) * | 2006-09-29 | 2010-05-12 | 上海化工研究院天地科技发展有限公司 | Method of preprocessing ultrahigh molecular weight polyethylene for spinning |
| CN101575743B (en) * | 2008-05-05 | 2011-04-13 | 宁波荣溢化纤科技有限公司 | Preparation method of spinning solution of ultra-high molecular weight polyethylene fiber |
| CN101629323B (en) * | 2008-07-17 | 2011-07-27 | 宁波荣溢化纤科技有限公司 | Method for conveying spinning suspension of ultra-high molecular weight polyethylene fiber |
| WO2012025034A1 (en) * | 2010-08-24 | 2012-03-01 | 北京同益中特种纤维技术开发有限公司 | Method for preparing spinning solution of ultra-high molecular weight polyethylene fiber |
| CN101724921B (en) * | 2009-11-26 | 2012-11-21 | 宁波大成新材料股份有限公司 | Process for evenly preparing spinning by using ultrahigh molecular weight polyethylene high-shearing solution |
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2001
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