CN106832160A - A kind of production method of α polyformaldehyde - Google Patents
A kind of production method of α polyformaldehyde Download PDFInfo
- Publication number
- CN106832160A CN106832160A CN201710106525.7A CN201710106525A CN106832160A CN 106832160 A CN106832160 A CN 106832160A CN 201710106525 A CN201710106525 A CN 201710106525A CN 106832160 A CN106832160 A CN 106832160A
- Authority
- CN
- China
- Prior art keywords
- polymerization
- polyformaldehyde
- high intensity
- polymerization machine
- formaldehyde
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 229920006324 polyoxymethylene Polymers 0.000 title claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims abstract description 121
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 100
- 230000018044 dehydration Effects 0.000 claims abstract description 19
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 19
- 238000003756 stirring Methods 0.000 claims abstract description 17
- 230000001404 mediated effect Effects 0.000 claims abstract description 9
- 230000005540 biological transmission Effects 0.000 claims abstract description 6
- 238000001035 drying Methods 0.000 claims abstract description 6
- 238000004898 kneading Methods 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 abstract description 7
- 239000003999 initiator Substances 0.000 abstract description 3
- 238000001125 extrusion Methods 0.000 abstract 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 8
- 229930040373 Paraformaldehyde Natural products 0.000 description 5
- 229920002866 paraformaldehyde Polymers 0.000 description 5
- -1 polyformaldehyde Chemical compound 0.000 description 5
- 238000012360 testing method Methods 0.000 description 4
- BGJSXRVXTHVRSN-UHFFFAOYSA-N 1,3,5-trioxane Chemical compound C1OCOCO1 BGJSXRVXTHVRSN-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- DHKHKXVYLBGOIT-UHFFFAOYSA-N 1,1-Diethoxyethane Chemical compound CCOC(C)OCC DHKHKXVYLBGOIT-UHFFFAOYSA-N 0.000 description 1
- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000004425 Makrolon Substances 0.000 description 1
- 239000004677 Nylon Substances 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 229920001807 Urea-formaldehyde Polymers 0.000 description 1
- 239000011354 acetal resin Substances 0.000 description 1
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000002964 excitative effect Effects 0.000 description 1
- 229920002313 fluoropolymer Polymers 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 125000005704 oxymethylene group Chemical group [H]C([H])([*:2])O[*:1] 0.000 description 1
- 229920001568 phenolic resin Polymers 0.000 description 1
- 239000005011 phenolic resin Substances 0.000 description 1
- 229920000515 polycarbonate Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- ODGAOXROABLFNM-UHFFFAOYSA-N polynoxylin Chemical compound O=C.NC(N)=O ODGAOXROABLFNM-UHFFFAOYSA-N 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 229920005992 thermoplastic resin Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G2/00—Addition polymers of aldehydes or cyclic oligomers thereof or of ketones; Addition copolymers thereof with less than 50 molar percent of other substances
- C08G2/08—Polymerisation of formaldehyde
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G6/00—Condensation polymers of aldehydes or ketones only
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyoxymethylene Polymers And Polymers With Carbon-To-Carbon Bonds (AREA)
Abstract
The present invention discloses a kind of production method of α polyformaldehyde, it is characterised in that comprise the following steps：Polymerization is stirred when dehydration is vacuumized during the formaldehyde that concentration is 50%~80% is added into low-intensity polymerization machine, preliminary polymerization product is obtained；Above-mentioned preliminary polymerization product is sent to high intensity by extruder and mediates polymerization machine porch, dehydration is vacuumized in transmission；While preliminary polymerization product input high intensity mediates polymerization machine, polymerization machine porch is mediated in high intensity add the formaldehyde that temperature is 50~90 DEG C, concentration is 50%~80%, dehydration is vacuumized while stirring, polymerization machine exit extrusion is mediated from high intensity, drying is crushed again, that is, the α polyformaldehyde is obtained.It is not required to make formaldehyde multi-step polymerization by adding any initiator, the anhydrous α polyformaldehyde of system, whole production operation is simple, low production cost, in can be widely applied to the production of polyformaldehyde, polymethoxy dimethyl ether etc..
Description
Technical field
The present invention relates to chemical production field, and in particular to a kind of production method of α-polyformaldehyde.
Background technology
Formaldehyde (molecular formula：HCHO) be also known as formaldehyde, be simplest aldehydes, be under normal circumstances it is a kind of flammable, colourless and
Gas excitatory.Soluble in water, alcohol and ether；Formaldehyde is a kind of important Organic Ingredients, is mainly used in plastics industry (as made
Phenolic resin, urea-formaldehyde plastics-electricity are beautiful, polyformaldehyde), synthetic fibers (such as synthesis vinylon-polyvinyl formal), leather work
Industry, medicine, dyestuff etc.；Storage is easily muddy long when colder for formaldehyde liquid, and paraformaldehyde precipitation is then formed in low temperature.Have during evaporation
A part of formaldehyde effusion, but majority becomes paraformaldehyde.
With industrial expansion, the requirement more and more higher of the deep processed product PARA FORMALDEHYDE PRILLS(91,95) of formaldehyde, particularly polyformaldehyde, poly- first
The production of epoxide dimethyl ether, it is desirable to which formaldehyde substantially can not be aqueous；But only with simply during Formaldehyde Production treatment
Rectifying cannot be the moisture discharge being mixed with formaldehyde；If desired anhydrous formaldehyde typically uses metaformaldehyde solution in existing industrial production
Consor produce anhydrous formaldehyde, but the production cost of metaformaldehyde is very high, so as to also improve anhydrous formaldehyde production cost and
The cost of the downstream product of anhydrous formaldehyde.
So be badly in need of at present it is a kind of can adapt in the production method of industrial anhydrous formaldehyde, reduce polyformaldehyde, poly-
The production cost of the formaldehyde downstream product such as methoxyl group dimethyl ether.
The content of the invention
The present invention proposes a kind of production method of α-polyformaldehyde regarding to the issue above, produces anhydrous formaldehyde, operating method letter
Singly it is not required to add any initiator, production cost can be greatly lowered.
A kind of production method of α-polyformaldehyde, comprises the following steps：
(1) polymerization is stirred when dehydration is vacuumized in the formaldehyde that concentration is 50%~80% being added into low-intensity polymerization machine,
Obtain preliminary polymerization product；
(2) above-mentioned preliminary polymerization product is sent to high intensity by extruder and mediates polymerization machine porch, in transmission
Vacuumize dehydration；
(3) while preliminary polymerization product input high intensity mediates polymerization machine, polymerization machine porch is mediated in high intensity
The formaldehyde that temperature is 50~90 DEG C, concentration is 50%~80% is added, dehydration is vacuumized while stirring, mediated from high intensity and be polymerized
Machine exit is extruded, then crushes drying, that is, the α-polyformaldehyde is obtained.
Further, in step (1), the low-intensity polymerization machine is twin-screw polymerization machine, and now formaldehyde viscosity is relatively low, double spiral shells
The stirring intensity of bar polymerization machine is smaller, and formaldehyde can be polymerized while stirring, produces the less preliminary polymerization product of the degree of polymerization.
Further, in step (1), the rotating speed of the low-intensity polymerization machine is 20~80r/min, unfavorable if rotating speed is too low
It is well mixed in low-intensity polymerization machine in formaldehyde, rotating speed is too high, is unfavorable for the polymerization of formaldehyde.
Further, in step (1), the formaldehyde stirs 4~8h of polymerization in the low-intensity polymerization machine, makes formaldehyde preliminary
Polymerization, the time, too short oxymethylene polymerization was insufficient, and the bigger viscosity of the degree of polymerization of mixing time then formaldehyde more long is bigger, now low-intensity
Polymerization machine is unable to reach the purpose of stirring because stirring intensity is smaller.
Further, in step (2), the extruder is single screw extruder, double-screw type extruder or multiscrew
In formula extruder any one, the input of the extruder connects the output end of the low-intensity polymerization machine, the extruder
Output end connects the input that the high intensity mediates polymerization machine, and the preliminary polymerization product conveying in low-intensity polymerization machine is paramount
Intensity high intensity continues to be polymerized in mediating polymerization machine.
Further, in step (3), it is Dual-screw kneader that the high intensity mediates polymerization machine, stirs the effect of mixing more
It is good.
Further, in step (3), the rotating speed that the high intensity mediates polymerization machine is 20~80r/min, is sufficiently mixed stirring
Product.
Further, the preliminary polymerization thing mediates polymerization machine entrance and mediates polymerization machine to the high intensity from the high intensity
It is 2~5h to export, and promotes formaldehyde to be further polymerized.
Further, the mass ratio that the addition quality of the formaldehyde mediates preliminary polymerization product in polymerization machine with high intensity is 1:
2~1:5, it is ensured that preliminary polymerization product can flow in high intensity mediates polymerization machine.
Compared with prior art, the invention has the advantages that：
1st, concentration is the addition of 50%~80% high-concentration formaldehyde, is not required to add any initiator to make formaldehyde multistage poly-
Close, while reducing the moisture in preliminary polymerization product, reduce dehydration difficulty；
2nd, preliminary polymerization product enters when in high intensity kneading polymerization machine, and viscosity is larger, it is difficult to stir, and now adds
High temperature, the formalin of high concentration can reduce the viscosity of preliminary polymerization product, and promote formaldehyde to be further polymerized until reaching
To the required degree of polymerization；
3rd, obtained α-polyformaldehyde is not aqueous, and whole production operation is simple, and low production cost can be widely applied to poly- first
In the production of aldehyde, polymethoxy dimethyl ether etc..
Specific embodiment
The technical program is described further below in conjunction with specific embodiment, so that those skilled in the art can be suitable
Profit is implemented.
Embodiment 1
1st, a kind of production method of α-polyformaldehyde, comprises the following steps：
(1) in formaldehyde that concentration is 50% being added into twin-screw polymerization machine, polymerization stir when dehydration is vacuumized, adjusted pair
The rotating speed of polymerization extruder is 40r/min, kneads 4h, obtains preliminary polymerization product；
(2) single screw extruder input connects the output end of twin-screw polymerization machine, single screw extruder output end
Connection Dual-screw kneader input, is sent to above-mentioned preliminary polymerization product twin-screw and mediates by single screw extruder
Machine, single screw extruder vacuumizes dehydration in transmission；
(3) while preliminary polymerization product is input into Dual-screw kneader, temperature is added in Dual-screw kneader porch
It is the formaldehyde that 90 DEG C, concentration are 80%, dehydration is vacuumized while stirring, 5h is mediated, wherein in the addition of formaldehyde and kneader
The mass ratio of preliminary polymerization thing is 1:2, mediate the product for terminating and extruded from Dual-screw kneader exit, then crush drying, i.e.,
α-the polyformaldehyde is obtained.
2nd, melt flow rate (MFR) test
Melt Flow Rate Measurer, melt mass flow rate (MFR), volume melt-flow for determining thermoplastic resin
Speed (MVR) and fusant density, it is applicable not only to the works such as melt temperature makrolon higher, nylon, fluoroplastics, polyarylsulfone (PAS)
Engineering plastics, are also applied for the relatively low plastics of the melt temperatures such as polyethylene, polystyrene, polypropylene, ABS resin, acetal resin
Test；Method of testing is under uniform temperature and load, by calculating the every 10 minutes quality or body by standard mouth mold of melt
Product, so as to draw the flow rate of melt, its numerical value can characterize viscosity flow characteristic of the thermoplastic in molten condition.
α-the polyformaldehyde that will be prepared in the present embodiment carries out melt flow rate (MFR) test, tests the melt quality of α-polyformaldehyde
Flow rate (MFR), with polyformaldehyde and paraformaldehyde reference, measures：
(1) paraformaldehyde is low polymerization degree formaldehyde, and the degree of polymerization is 8~100, because the degree of polymerization is low, then in melt flows speed
Heating is gasified in rate instrument, does not measure melt mass flow rate；
(2) more than 1000, the melting means number for measuring polyformaldehyde is the degree of polymerization of polyformaldehyde：9g/min；
(3) the melting means number of the present embodiment α-polyformaldehyde is：30g/min；So as to push away the technical program polyformaldehyde
Polymerization scope is 300~500, is α-polyformaldehyde.
Embodiment 2
(1) in formaldehyde that concentration is 60% being added into twin-screw polymerization machine, polymerization stir when dehydration is vacuumized, adjusted pair
The rotating speed of polymerization extruder is 20r/min, kneads 6h, obtains preliminary polymerization product；
(2) double-screw type extruder input connects the output end of twin-screw polymerization machine, double-screw type extruder output end
Connection Dual-screw kneader input, is sent to above-mentioned preliminary polymerization product twin-screw and mediates by double-screw type extruder
Machine, double-screw type extruder vacuumizes dehydration in transmission；
(3) while preliminary polymerization product is input into Dual-screw kneader, temperature is added in Dual-screw kneader porch
It is the formaldehyde that 50 DEG C, concentration are 50%, dehydration is vacuumized while stirring, 4h is mediated, wherein in the addition of formaldehyde and kneader
The mass ratio of preliminary polymerization thing is 1:4, mediate the product for terminating and extruded from Dual-screw kneader exit, then crush drying, i.e.,
α-the polyformaldehyde is obtained.
Embodiment 3
(1) in formaldehyde that concentration is 80% being added into twin-screw polymerization machine, polymerization stir when dehydration is vacuumized, adjusted pair
The rotating speed of polymerization extruder is 80r/min, kneads 8h, obtains preliminary polymerization product；
(2) multiscrew formula extruder input connects the output end of twin-screw polymerization machine, multiscrew formula extruder output end
Connection Dual-screw kneader input, is sent to above-mentioned preliminary polymerization product twin-screw and mediates by multiscrew formula extruder
Machine, multiscrew formula extruder vacuumizes dehydration in transmission；
(3) while preliminary polymerization product is input into Dual-screw kneader, temperature is added in Dual-screw kneader porch
It is the formaldehyde that 80 DEG C, concentration are 60%, dehydration is vacuumized while stirring, 8h is mediated, wherein in the addition of formaldehyde and kneader
The mass ratio of preliminary polymerization thing is 1:5, mediate the product for terminating and extruded from Dual-screw kneader exit, then crush drying, i.e.,
α-the polyformaldehyde is obtained.
Above-mentioned implementation method is only the preferred embodiment of the present invention, it is impossible to limit the scope of protection of the invention with this,
The change and replacement of any unsubstantiality that those skilled in the art is done on the basis of invention belong to the present invention and want
Seek the scope of protection.
Claims (9)
1. a kind of production method of α-polyformaldehyde, it is characterised in that comprise the following steps：
(1) polymerization is stirred when dehydration is vacuumized in the formaldehyde that concentration is 50%~80% being added into low-intensity polymerization machine, is obtained just
Step polymerizate；
(2) above-mentioned preliminary polymerization product is sent to high intensity by extruder and mediates polymerization machine porch, take out true in transmission
Sky dehydration；
(3) while preliminary polymerization product is input into the high intensity and mediates polymerization machine, polymerization machine porch is mediated in high intensity
The formaldehyde that temperature is 50~90 DEG C, concentration is 50%~80% is added, dehydration is vacuumized while stirring, mediated from high intensity and be polymerized
Machine exit is extruded, then crushes drying, that is, the α-polyformaldehyde is obtained.
2. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (1), the low-intensity
Polymerization machine is twin-screw polymerization machine.
3. a kind of production method of α-polyformaldehyde according to claim 2, it is characterised in that in step (1), the low-intensity
The rotating speed of polymerization machine is 20~80r/min.
4. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (1), the formaldehyde exists
4~8h of polymerization is stirred in the low-intensity polymerization machine.
5. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (2), the extruder
For in single screw extruder, double-screw type extruder or multiscrew formula extruder any one, the input of the extruder
The output end of the low-intensity polymerization machine is connected, the output end of the extruder connects the input that the high intensity mediates polymerization machine
End.
6. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (3), the high intensity
Kneading polymerization machine is Dual-screw kneader.
7. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (3), the high intensity
The rotating speed for mediating polymerization machine is 20~80r/min.
8. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that described preliminary poly- in step (3)
It is 2~5h that compound mediate polymerization machine entrance to mediate polymerization machine outlet from the high intensity to the high intensity.
9. a kind of production method of α-polyformaldehyde according to claim 1, it is characterised in that in step (3), the formaldehyde
The mass ratio for adding quality to mediate preliminary polymerization product in polymerization machine with high intensity is 1:2~1:5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710106525.7A CN106832160A (en) | 2017-02-27 | 2017-02-27 | A kind of production method of α polyformaldehyde |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710106525.7A CN106832160A (en) | 2017-02-27 | 2017-02-27 | A kind of production method of α polyformaldehyde |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106832160A true CN106832160A (en) | 2017-06-13 |
Family
ID=59134317
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710106525.7A Pending CN106832160A (en) | 2017-02-27 | 2017-02-27 | A kind of production method of α polyformaldehyde |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106832160A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2568016A (en) * | 1949-03-12 | 1951-09-18 | Celanese Corp | Formaldehyde conversion |
| US2768994A (en) * | 1952-08-30 | 1956-10-30 | Du Pont | Polyoxymethylenes |
| US2775619A (en) * | 1953-09-25 | 1956-12-25 | Galat Alexander | Preparation of paraformaldehyde |
| US3342779A (en) * | 1963-07-03 | 1967-09-19 | Toyo Koatsu Ind Inc | Process for producing alphapolyoxymethylene |
| JP2011116862A (en) * | 2009-12-03 | 2011-06-16 | Asahi Kasei Chemicals Corp | Method for producing polyacetal resin composition and polyacetal resin composition |
-
2017
- 2017-02-27 CN CN201710106525.7A patent/CN106832160A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2568016A (en) * | 1949-03-12 | 1951-09-18 | Celanese Corp | Formaldehyde conversion |
| US2768994A (en) * | 1952-08-30 | 1956-10-30 | Du Pont | Polyoxymethylenes |
| US2775619A (en) * | 1953-09-25 | 1956-12-25 | Galat Alexander | Preparation of paraformaldehyde |
| US3342779A (en) * | 1963-07-03 | 1967-09-19 | Toyo Koatsu Ind Inc | Process for producing alphapolyoxymethylene |
| JP2011116862A (en) * | 2009-12-03 | 2011-06-16 | Asahi Kasei Chemicals Corp | Method for producing polyacetal resin composition and polyacetal resin composition |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101051015A (en) | Novel high polymer system rheological performance detector | |
| WO2020143208A1 (en) | Method and device for directly preparing foamed polylactic acid article using polylactic acid polymer melt | |
| US10889666B2 (en) | Molecular modification of polyethylene resin | |
| CN119752075A (en) | Production processes and equipment for processing polyvinyl alcohol | |
| Ville et al. | Influence of extrusion conditions on fiber breakage along the screw profile during twin screw compounding of glass fiber-reinforced PA | |
| Rosales et al. | Grafting of polyethylenes by reactive extrusion. I. Influence on the molecular structure | |
| CN100493885C (en) | Supercritical fluid assisted polymer material extrusion molding machine | |
| US20190337211A1 (en) | Distributive and dispersive mixing devices | |
| CN1769030A (en) | Method of manufacturing profiles from thermoplastic material | |
| Gibson et al. | Shear and extensional flow of reinforced plastics in injection molding. I. Effects of temperature and shear rate with bulk molding compound | |
| CN1959372A (en) | Rheological behavior mensuration instrument for system of supercutical fluid - polymer | |
| CN106832160A (en) | A kind of production method of α polyformaldehyde | |
| Lepschi et al. | Determining the residence time distribution of various screw elements in a co-rotating twin-screw extruder by means of fluorescence spectroscopy | |
| US11623381B2 (en) | Sub-critical gas-assisted processing of a polymer blend | |
| CN107936385A (en) | A kind of low-temperature impact-resistant PPR pipe and preparation method thereof | |
| Carrino et al. | Effect of filler content and temperature on steady‐state shear flow of wood/high density polyethylene composites | |
| CN104497471A (en) | Method for preparing wood-plastic composite material through subcritical water extrusion | |
| WO2021237655A1 (en) | Liquid additive assisted polymer extrusion and blending method and device and use thereof | |
| JP5536704B2 (en) | Method for producing glass fiber reinforced thermoplastic resin composition pellets | |
| CN215150811U (en) | Extruder of plasticization modified nylon 12 granule material for production car pipeline | |
| CN103965551A (en) | Formula and processing technology of PP-R pipe | |
| EP4353436A1 (en) | Kneading apparatus | |
| Thompson et al. | Experiments and flow analysis of a micropelletizing die | |
| Mayrick et al. | Extrusion characteristics of poly (vinyl chloride) | |
| Mudalamane et al. | Experimental characterization of fill length behavior in extruders |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170613 |