CN106749814A - One kind coating level ethylene vinyl acetate copolymer and its production technology - Google Patents
One kind coating level ethylene vinyl acetate copolymer and its production technology Download PDFInfo
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- CN106749814A CN106749814A CN201611055809.XA CN201611055809A CN106749814A CN 106749814 A CN106749814 A CN 106749814A CN 201611055809 A CN201611055809 A CN 201611055809A CN 106749814 A CN106749814 A CN 106749814A
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
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Abstract
The present invention relates to one kind coating level ethylene ethyl acetate copolymer and its production technology, belong to technical field of new material preparation.Polymer grade ethylene enters reactor after being compressed through compressor in certain proportion with vinylacetate, isobutene is molecular weight regulator, add initiator peroxidating tert-butyl isobutyrate (C27) that concentration is 20% and the tert-Butyl peroxypivalate (C32) that concentration is 30%, the successive reaction in reactor, after being separated through high-pressure separator and low pressure separator, product ethylene vinyl acetate co-polymer (EVA) is obtained after extruder grain.The present invention prepare coating level ethylene vinyl acetate copolymer, with long chain branching degree it is high, fisheye is controlled the characteristics of.
Description
Technical field
The present invention relates to one kind coating level ethylene-vinyl acetate copolymer and its production technology, belong to new material preparation
Technical field.
Background technology
Ethylene-vinyl acetate copolymer (EVA) is the copolymer of ethene and vinylacetate (VA).It is soft relative to other
Property material (such as polyurethane, silicon rubber, fluorinated vinyl resin), EVA as a kind of flexible body, with easy processing, compatibility
The advantages such as good, amount of deflection is high, pliability is good, anti-aging, the stress cracking that can be resisted under natural environment, having been developed as industry should
Classical kind in, in injection extrusion molding article, foaming product, oriented film, electric wire and cable jacket adhesive and fluid sealant
Turn into indispensable kind Deng field, be widely used in the fields such as plastics, rubber, fiber and adhesive.
EVA is used as a kind of unformed plastics, although elastic good, good fluidity, pliability are good, but its lustrous surface
Difference, mechanical strength are low.
Coating level ethylene-vinyl acetate copolymer distinguishing feature is high to the requirement of product fisheye, therefore in production process
It is middle to need fisheye quantity in strict control product.
The content of the invention
The invention provides one kind coating level ethylene-vinyl acetate copolymer and its production technology, in overcoming product
Fisheye problem high.Technical scheme is as follows：
A kind of production technology for applying level ethylene-vinyl acetate copolymer, comprises the following steps that：
(1) pressure is the polymer grade ethylene of 3.5-3.8MPaG, after heated device is heated to 30-35 DEG C, into first compression
Machine, first compression machine is divided into two-stage, and inside is provided with first compression machine one-level aftercooler, and the outlet of first compression machine is provided with once
Two grades of deep freezers of two grades of aftercoolers of compressor and first compression machine, after polymer grade ethylene compresses through first compression machine, pressure is
30MPaG, by polymer grade ethylene after two grades of deep freezers of two grades of aftercoolers of first compression machine and first compression machine temperature be 25-
35℃；
Preferably, pressure is the polymer grade ethylene of 3.7MPaG, after heated device is heated to 30 DEG C, into first compression machine,
First compression machine is divided into two-stage, and inside is provided with first compression machine one-level aftercooler, and the outlet of first compression machine is provided with once presses
Two grades of deep freezers of two grades of aftercoolers of contracting machine and first compression machine, after polymer grade ethylene compresses through first compression machine, pressure is
30MPaG, by polymer grade ethylene after two grades of deep freezers of two grades of aftercoolers of first compression machine and first compression machine temperature be 28
℃。
(2) by the polymer grade ethylene of first compression machine at secondary compressor import with pressure for 34MPaG regulator
The comonomer vinylacetate (VA) that isobutene and water content are 60ppm, pressure is 34MPaG is mixed, polymer grade second
Alkene, vinylacetate, the flow-rate ratio (t/h of isobutene:t/h:T/h it is) 82：8：0.12 mixed gas enter secondary compressor, warp
The pressure for crossing mixed gas after secondary compressor is compressed is 165MPa, and temperature is 55-65 DEG C；
Preferably, it is 165MPa by the pressure of mixed gas after secondary compressor compression, temperature is 58 DEG C.
(3) mixed gas after being compressed by secondary compressor are preheated by reactor feed cooler and reactor feed
Device/deep freezer, reduces the temperature to 15 DEG C, be divided into 1 from bottom to top into reactor, in reactor, 2,3,4,5,6,7,8,9,10,
11 reaction zones, in reactor start-up, the temperature of mixed gas is heated to 140 DEG C, then 5,7,9 and 11 in reactor
Reaction zone injects peroxide initiator, and the initiator of 5 reaction zones is the tert-Butyl peroxypivalate that mass concentration is 30%,
7th, the initiator of 9 and 11 reaction zones is the peroxidating tert-butyl isobutyrate that mass concentration is 20%, and 5,7,9 and 11 reaction zones draw
Send out the flow-rate ratio (kg/h of agent:kg/h:kg/h:Kg/h it is) 1:1:1:The temperature of 2,1 reaction zones is 211 DEG C, the temperature of 2 reaction zones
Be 208 DEG C, the temperature of 3 reaction zones is 205 DEG C, the temperature of 4 reaction zones is 205 DEG C, the temperature of 5 reaction zones is 204 DEG C, 6,7,8,
9th, the temperature of 10 and 11 reaction zones is 204 DEG C, and the pressure of reactor is 1590bar；
In the present invention, reactor feed cooler makees cooling medium, reactor feed preheater/deep freezer using recirculated water
The chilled water for using 6 DEG C is cooling medium.
In the present invention, the reactor body is provided with four rupture disks, and rupture disk is used for overpressure protection, two rupture disks
Outlet be connected with concetrated pipe chimney respectively, burst pressure is set to 225MPaG, and the outlet of two other rupture disk is extended to instead
Answer outside dam, the pressure of explosion is set to 240MPaG.
(4) by reactor outlet ethylene-vinyl acetate copolymer (EVA) out, vinylacetate and polymer grade second
After the mixed gas of alkene are cooled down through cooler, temperature drops to 170-200 DEG C, the mixed gas after cooling, by high voltage relief valve
After step-down, first time separation is carried out into high-pressure separator, the pressure in high-pressure separator is 30MPaG, and temperature is 180-210
DEG C, ethylene-vinyl acetate copolymer, a small amount of polymer grade ethylene and a small amount of vinylacetate are from the bottom of high-pressure separator
Discharge, enters low pressure separator after low-voltage decompression valve depressurizes, and other mixed gas are discharged from the top of high-pressure separator, entered
Enter high-pressure recycle system；
Preferably, the pressure in high-pressure separator is 30MPaG, and temperature is 210 DEG C.
(5) pressure in low pressure separator is 0.05-0.12MPaG, and temperature is 160-180 DEG C, ethylene-vinyl acetate
Copolymer is directly entered extruder and carries out extruder grain by the bottom discharge of low pressure separator, obtains final product ethylene-vinyl acetate and is total to
Copolymer product；Other gases are by being discharged into low pressure recycle system at the top of low pressure separator；Discharged by low pressure recycle system
Gas enters purging air compressor, and gas pressure is boosted to about 3.6MPaG, purge gass by purging air compressor from about 0.02MPaG
Compressor outlet major part ethylene gas feeding first compression machine entrance, the ethylene gas of 3 (wt) % are being purged as off-gas
The outlet of air compressor three-level is separated, and the off-gas refined unit outside feeding battery limit (BL) carries out purified treatment；
Preferably, the pressure in low pressure separator is 0.11MPaG, and temperature is 180 DEG C.
The high-pressure recycle system is：From high-pressure separator top, gas out is cooled down by waste heat boiler, while producing
Raw 0.35MPaG low-pressure steams；The gas cooled down by the pot that gives up follows Gas Cooler by three sections high again, passes through again after each section of cooling
Height follows gas separating device, and oligomer is separated, and the gas isolated returns to the recycling of secondary compressor entrance；From Gao Xun
The wax and residuals separated in gas separating device are discharged into wax blowdown vessel；
The low pressure recycle system is：From low pressure separator top gas out by polymer knockout drum, purge gass
Enter purge gass compressor after cooler and purge gass deep freezer；Purging Gas Cooler and purge gass deep freezer are two and vertical change
Hot device, is respectively adopted recirculated water and chilled water as cooling medium.
The wax exhaust system, including wax discharge tank body, wax collecting vessel, steamtraced piping, high-low pressure steam branch pipe and
High steam branch pipe, wax discharge tank base is connected by automatic switch valve with wax collecting vessel, and wax discharge tank wall is provided with
Steamtraced piping, high steam branch pipe is connected by jet chimney with steamtraced piping, and high-low pressure steam branch pipe is by steaming
Steam pipe road is connected with steamtraced piping, and valve is equipped with high-low pressure steam branch pipe and high steam branch pipe, and high-low pressure steams
Vapour branch pipe and high steam branch pipe are pipeline arranged side by side.Wax enters wax and discharges tank body, and gas enters low pressure recycle system, wax from top
From tank bottom discharge.
In the prior art, VA is separated out easily from wax exhaust system, and discharging tank body by wax is emitted into wax collecting vessel, both makes
Causing material consumption again into environmental pollution increases.In the present invention, transformed by the novelty to wax exhaust system, increased high steam
Branch pipe, had not only avoided VA and has separated out but also product quality will not be impacted.
The present invention has advantages below compared with prior art：
Coating level ethylene-vinyl acetate copolymer prepared by the present invention, with long chain branching degree is high, fisheye is controlled
Feature.
Brief description of the drawings
Fig. 1 is wax exhaust system schematic diagram in the present invention.
Symbol description：
1. wax discharges tank body, 2. wax collecting vessel, 3. steamtraced piping, 4. high-low pressure steam branch pipe, 5. high steam branch
Pipe.
Specific embodiment
Further describe the present invention with reference to specific embodiment, advantages of the present invention and feature will be with description and
It is apparent.But embodiment is only exemplary, does not constitute any limitation to the scope of the present invention.Those skilled in the art should
It should be appreciated that, the details of technical solution of the present invention and form can be repaiied without departing from the spirit and scope of the invention
Change or replace, but these modifications and replacement are each fallen within protection scope of the present invention.
A kind of production technology for applying level ethylene-vinyl acetate copolymer of embodiment 1, comprises the following steps that：
(1) pressure is the polymer grade ethylene of 3.7MPaG, after heated device is heated to 30 DEG C, into first compression machine, once
Compressor is divided into two-stage, and inside is provided with first compression machine one-level aftercooler, and the outlet of first compression machine is provided with first compression machine
Two grades of deep freezers of two grades of aftercoolers and first compression machine, after polymer grade ethylene compresses through first compression machine, pressure is 30MPaG, warp
The temperature for crossing polymer grade ethylene after two grades of deep freezers of two grades of aftercoolers of first compression machine and first compression machine is 28 DEG C；
(2) by the polymer grade ethylene of first compression machine at secondary compressor import with pressure for 34MPaG regulator
The comonomer vinylacetate (VA) that isobutene and water content are 60ppm, pressure is 34MPaG is mixed, polymer grade second
Alkene, vinylacetate, the flow-rate ratio (t/h of isobutene:t/h:T/h it is) 82：8：0.12, mixed gas enter secondary compressor,
It is 165MPa by the pressure of mixed gas after secondary compressor compression, temperature is 58 DEG C；
(3) mixed gas after being compressed by secondary compressor are preheated by reactor feed cooler and reactor feed
Device/deep freezer, after reducing the temperature to 15 DEG C, be divided into 1 from bottom to top into reactor, in reactor, 2,3,4,5,6,7,8,9,
10th, 11 reaction zone, in reactor start-up, the temperature of mixed gas is heated to 140 DEG C, then 5,7,9 and in reactor
11 reaction zones inject peroxide initiator, and the initiator of 5 reaction zones is the peroxidating tertiary fourth of neopentanoic acid that mass concentration is 30%
Ester, the initiator of 7,9 and 11 reaction zones is the peroxidating tert-butyl isobutyrate that mass concentration is 20%, 5,7,9 and 11 reaction zones
Flow-rate ratio (the kg/h of initiator:kg/h:kg/h:Kg/h it is) 1:1:1:The temperature of 2,1 reaction zones is 211 DEG C, the temperature of 2 reaction zones
It is 208 DEG C to spend, and the temperature of 3 reaction zones is 205 DEG C, and the temperature of 4 reaction zones is 205 DEG C, and the temperature of 5 reaction zones is 204 DEG C, 6,7,
8th, the temperature of 9,10 and 11 reaction zones is 204 DEG C, and the pressure of reactor is 1590bar；
Reactor feed cooler makees cooling medium using recirculated water, and reactor feed preheater/deep freezer is using 6 DEG C
Chilled water is cooling medium.
The reactor body is provided with four rupture disks, and rupture disk is used for overpressure protection, two outlets of rupture disk point
It is not connected with concetrated pipe chimney, burst pressure is set to 225MPaG, the outlet of two other rupture disk is extended to outside reaction dam,
The pressure of explosion is set to 240MPaG.
(4) by reactor outlet ethylene-vinyl acetate copolymer (EVA) out, vinylacetate and polymer grade second
After the mixed gas of alkene are cooled down through cooler, temperature drops to 170-200 DEG C, the mixed gas after cooling, by high-pressure decompression valve
After step-down, first time separation is carried out into high-pressure separator, the pressure in high-pressure separator is 30MPaG, temperature is 210 DEG C, second
Alkene-vinyl acetate co-polymer, a small amount of polymer grade ethylene and a small amount of vinylacetate are discharged from the bottom of high-pressure separator,
Enter low pressure separator after low-voltage decompression valve depressurizes, other mixed gas are discharged from the top of high-pressure separator, into height
The pressure circulatory system；
(5) pressure in low pressure separator is 0.11MPaG, and temperature is 180 DEG C, and ethylene-vinyl acetate copolymer is by low
Pressing the bottom discharge of separator to be directly entered extruder carries out extruder grain, obtains final product ethylene-vinyl acetate copolymer product；Its
Its gas is by being discharged into low pressure recycle system at the top of low pressure separator；The gas discharged by low pressure recycle system enters purging
Gas pressure is boosted to about 3.6MPaG by air compressor, purging air compressor from about 0.02MPaG, and purge gass compressor outlet is big
Part ethylene gas feeding first compression machine entrance, the ethylene gas of 3 (wt) % are purging air compressor three-level as off-gas
Outlet is separated, and the off-gas refined unit outside feeding battery limit (BL) carries out purified treatment；
The high-pressure recycle system is：From high-pressure separator top, gas out is cooled down by waste heat boiler, while producing
Raw 0.35MPaG low-pressure steams；The gas cooled down by the pot that gives up follows Gas Cooler by three sections high again, passes through again after each section of cooling
Height follows gas separating device, and oligomer is separated, and the gas isolated returns to the recycling of secondary compressor entrance；From Gao Xun
The wax and residuals separated in gas separating device are discharged into wax exhaust system；
The low pressure recycle system is：From low pressure separator top gas out by polymer knockout drum, purge gass
Enter purge gass compressor after cooler and purge gass deep freezer；Purging Gas Cooler and purge gass deep freezer are two and vertical change
Hot device, is respectively adopted recirculated water and chilled water as cooling medium.
The wax exhaust system of embodiment 2
On the basis of embodiment 1, as shown in figure 1, the wax exhaust system, including wax discharge tank body 1, wax collecting vessel 2,
Steamtraced piping 3, high-low pressure steam branch pipe 4 and high steam branch pipe 5, wax discharge tank body 1 bottom by automatic switch valve with
Wax collecting vessel 2 is connected, and the wax discharge side wall of tank body 1 is provided with steamtraced piping 3, high steam branch pipe 5 by jet chimney with
Steamtraced piping 3 is connected, and high-low pressure steam branch pipe 4 is connected by jet chimney with steamtraced piping 3, high-low pressure steam branch
Valve is equipped with pipe 4 and high steam branch pipe 5, and high-low pressure steam branch pipe 4 and high steam branch pipe 5 are pipeline arranged side by side.Wax
Tank body is discharged into wax, gas enters low pressure recycle system from top, and wax is discharged from tank bottom.
Test example 1 carries out performance test by the coating level ethylene-ethyl acetate copolymer that EM methods are prepared to the present invention, ties
Fruit is as shown in table 1：
Table 1
Claims (9)
1. it is a kind of apply level ethylene-vinyl acetate copolymer production technology, it is characterised in that the specific steps of production technology
It is as follows：
(1) pressure is the polymer grade ethylene of 3.5-3.8MPaG, after heated device is heated to 30-35 DEG C, into first compression machine,
First compression machine is divided into two-stage, and inside is provided with first compression machine one-level aftercooler, and the outlet of first compression machine is provided with once presses
Two grades of deep freezers of two grades of aftercoolers of contracting machine and first compression machine, after polymer grade ethylene compresses through first compression machine, pressure is
30MPaG, by polymer grade ethylene after two grades of deep freezers of two grades of aftercoolers of first compression machine and first compression machine temperature be 25-
35℃；
(2) by the polymer grade ethylene of first compression machine at secondary compressor import with pressure for 34MPaG regulator isobutyl
The comonomer vinylacetate (VA) that alkene and water content are 60ppm, pressure is 34MPaG is mixed, polymer grade ethylene,
Flow-rate ratio (the t/h of vinylacetate, isobutene:t/h:T/h it is) 82：8：0.12, mixed gas enter secondary compressor, pass through
The pressure of mixed gas is 165MPa after secondary compressor compression, and temperature is 55-65 DEG C；
(3) mixed gas after being compressed by secondary compressor are by reactor feed cooler and reactor feed preheater/depth
Cooler, after reducing the temperature to 15 DEG C, into reactor, 1,2,3,4,5,6,7,8,9,10,11 is divided into reactor from bottom to top
Reaction zone, in reactor start-up, the temperature of mixed gas is heated to 140 DEG C, and then 5,7,9 and 11 in reactor are anti-
Area is answered to inject peroxide initiator, the initiator of 5 reaction zones is the tert-Butyl peroxypivalate that mass concentration is 30%, 7,
The initiator of 9 and 11 reaction zones is the peroxidating tert-butyl isobutyrate that mass concentration is 20%, and 5,7,9 and 11 reaction zones trigger
Flow-rate ratio (the kg/h of agent:kg/h:kg/h:Kg/h it is) 1:1:1:The temperature of 2,1 reaction zones is 211 DEG C, and the temperature of 2 reaction zones is
208 DEG C, the temperature of 3 reaction zones is 205 DEG C, and the temperature of 4 reaction zones is 205 DEG C, and the temperature of 5 reaction zones is 204 DEG C, 6,7,8,9,
The temperature of 10 and 11 reaction zones is 204 DEG C, and the pressure of reactor is 1590bar；
(4) by reactor outlet ethylene-vinyl acetate copolymer (EVA) out, vinylacetate and polymer grade ethylene
After mixed gas are cooled down through cooler, temperature drops to 170-200 DEG C, the mixed gas after cooling, is depressured by high-pressure decompression valve
Afterwards, first time separation is carried out into high-pressure separator, the pressure in high-pressure separator is 30MPaG, temperature is 180-210 DEG C, second
Alkene-vinyl acetate co-polymer, a small amount of polymer grade ethylene and a small amount of vinylacetate are discharged from the bottom of high-pressure separator,
Enter low pressure separator after low-voltage decompression valve depressurizes, other mixed gas are discharged from the top of high-pressure separator, into height
The pressure circulatory system；
The high-pressure recycle system is：From high-pressure separator top, gas out is cooled down by waste heat boiler, while producing
0.35MPaG low-pressure steams；The gas cooled down by the pot that gives up follows Gas Cooler by three sections high again, again through too high after each section of cooling
Gas separating device is followed, oligomer is separated, the gas isolated returns to the recycling of secondary compressor entrance；From Gao Xunqi
The wax and residuals separated in separator are discharged into wax exhaust system；
(5) pressure in low pressure separator is 0.05-0.12MPaG, and temperature is 160-180 DEG C, ethylene-vinyl acetate copolymerization
Thing is directly entered extruder and carries out extruder grain by the bottom discharge of low pressure separator, obtains final product ethylene-vinyl acetate copolymer
Product；Other gases are by being discharged into low pressure recycle system at the top of low pressure separator；The gas discharged by low pressure recycle system
Into purging air compressor, gas pressure is boosted to about 3.6MPaG, purge gass compression by purging air compressor from about 0.02MPaG
The most of ethylene gas feeding first compression machine entrance of machine outlet, the ethylene gas of 3 (wt) % are purging air pressure as off-gas
The outlet of contracting machine three-level is separated, and the off-gas refined unit outside feeding battery limit (BL) carries out purified treatment；
The low pressure recycle system is：From low pressure separator top gas out by polymer knockout drum, air cooling is purged
Enter purge gass compressor after device and purge gass deep freezer；Purging Gas Cooler and purge gass deep freezer are two vertical heat exchangings
Device, is respectively adopted recirculated water and chilled water as cooling medium.
2. production technology according to claim 1, it is characterised in that pressure is the polymerization of 3.7MPaG in the step (1)
Level ethene, after heated device is heated to 30 DEG C, into first compression machine, first compression machine is divided into two-stage, and inside is provided with once
Compressor one-level aftercooler, the outlet of first compression machine is provided with two grades of deep coolings of two grades of aftercoolers of first compression machine and first compression machine
Device, after polymer grade ethylene compresses through first compression machine, pressure is 30MPaG, is pressed by two grades of aftercoolers of first compression machine and once
The temperature of polymer grade ethylene is 28 DEG C after two grades of deep freezers of contracting machine.
3. production technology according to claim 1, it is characterised in that compressed by secondary compressor in the step (2)
The pressure of mixed gas is 165MPa afterwards, and temperature is 58 DEG C.
4. production technology according to claim 1, it is characterised in that reactor feed cooler is adopted in the step (3)
Make cooling medium with recirculated water, it is cooling medium that reactor feed preheater/deep freezer uses 6 DEG C of chilled water.
5. production technology according to claim 1, it is characterised in that set on reactor body described in the step (3)
There are four rupture disks, rupture disk is used for overpressure protection, and two outlets of rupture disk are connected with concetrated pipe chimney respectively, burst pressure
225MPaG is set to, the outlet of two other rupture disk is extended to outside reaction dam, and the pressure of explosion is set to 240MPaG.
6. production technology according to claim 1, it is characterised in that the pressure in step (4) high-pressure separator
It is 30MPaG, temperature is 210 DEG C.
7. production technology according to claim 1, it is characterised in that wax exhaust system in the step (4), including wax row
Tank body, wax collecting vessel, steamtraced piping, high-low pressure steam branch pipe and high steam branch pipe are put, wax discharge tank base passes through
Automatic switch valve is connected with wax collecting vessel, and wax discharge tank wall is provided with steamtraced piping, and high steam branch pipe is by steaming
Steam pipe road is connected with steamtraced piping, and high-low pressure steam branch pipe is connected by jet chimney with steamtraced piping, high-low pressure
Valve is equipped with steam branch pipe and high steam branch pipe, and high-low pressure steam branch pipe and high steam branch pipe are pipeline arranged side by side.
8. production technology according to claim 1, it is characterised in that the pressure in step (5) the mesolow separator
It is 0.11MPaG, temperature is 180 DEG C.
9. the coating level ethylene-vinyl acetate copolymer that prepared by the production technology as described in claim any one of 1-8.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611055809.XA CN106749814A (en) | 2016-11-25 | 2016-11-25 | One kind coating level ethylene vinyl acetate copolymer and its production technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611055809.XA CN106749814A (en) | 2016-11-25 | 2016-11-25 | One kind coating level ethylene vinyl acetate copolymer and its production technology |
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| Publication Number | Publication Date |
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| CN106749814A true CN106749814A (en) | 2017-05-31 |
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| CN201611055809.XA Withdrawn CN106749814A (en) | 2016-11-25 | 2016-11-25 | One kind coating level ethylene vinyl acetate copolymer and its production technology |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20190010260A1 (en) * | 2015-09-11 | 2019-01-10 | Exxonmobil Chemical Patents Inc. | High Pressure Polyethylene Product Cooling |
| CN113956380A (en) * | 2021-09-28 | 2022-01-21 | 国家能源集团宁夏煤业有限责任公司 | Carrier gas distribution, treatment and polymerization reaction system for polyolefin production process |
-
2016
- 2016-11-25 CN CN201611055809.XA patent/CN106749814A/en not_active Withdrawn
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20190010260A1 (en) * | 2015-09-11 | 2019-01-10 | Exxonmobil Chemical Patents Inc. | High Pressure Polyethylene Product Cooling |
| US10766984B2 (en) * | 2015-09-11 | 2020-09-08 | Exxonmobil Chemical Patents, Inc. | High pressure polyethylene product cooling |
| CN113956380A (en) * | 2021-09-28 | 2022-01-21 | 国家能源集团宁夏煤业有限责任公司 | Carrier gas distribution, treatment and polymerization reaction system for polyolefin production process |
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