CN108341895A - A kind of cohesion production technology of the parts ESBR precrosslinked rubber latex - Google Patents
A kind of cohesion production technology of the parts ESBR precrosslinked rubber latex Download PDFInfo
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- CN108341895A CN108341895A CN201710050902.XA CN201710050902A CN108341895A CN 108341895 A CN108341895 A CN 108341895A CN 201710050902 A CN201710050902 A CN 201710050902A CN 108341895 A CN108341895 A CN 108341895A
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- latex
- rubber latex
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- precrosslinked rubber
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08C—TREATMENT OR CHEMICAL MODIFICATION OF RUBBERS
- C08C1/00—Treatment of rubber latex
- C08C1/14—Coagulation
- C08C1/15—Coagulation characterised by the coagulants used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J3/00—Processes of treating or compounding macromolecular substances
- C08J3/24—Crosslinking, e.g. vulcanising, of macromolecules
- C08J3/26—Crosslinking, e.g. vulcanising, of macromolecules of latex
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J2309/00—Characterised by the use of homopolymers or copolymers of conjugated diene hydrocarbons
- C08J2309/06—Copolymers with styrene
- C08J2309/08—Latex
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- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
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- General Chemical & Material Sciences (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Abstract
A kind of cohesion production technology of parts ESBR precrosslinked rubber latex, belongs to Polymer Production Technology field.It is characterized in that, processing step is：Latex is added in the pretreating containers that rotating speed is 100rpm ~ 300rpm stirrings and carries out precrosslink；Precrosslinked rubber latex is mixed to get with uncrosslinked latex in static mixer and mixes latex, the mass ratio that precrosslinked rubber latex accounts for mixing latex is 3.5% ~ 15%；Epoxy glue milk flow enters collection surface, and mixing latex, flocculating agent, sulfuric acid, polymer coagulant are 100 with clear mass ratio is starched：0.008~0.013：0.9~1.4：0.073~0.092：32 ~ 38, aggregation temperature is 50 DEG C ~ 60 DEG C；Cohesion gained micelle is sent to drying box after being dehydrated, washing, and after drying box is dried to water content below 0.6%, is crushed, compound stalk forming.The problems such as glue particle is too small after the present invention solves blending part precrosslinked rubber latex, and cohesion slurry is clear muddy, and waste water COD is high.
Description
Technical field
A kind of cohesion production technology of parts ESBR precrosslinked rubber latex, belongs to Polymer Production Technology field.
Background technology
The requirement of high-performance tire is concentrated mainly on low-rolling-resistance and high wet-sliding resistant, three aspect performance of high-wearing feature
In balance, in order to realize the balance of three aspect performances, research worker both domestic and external is in the synthesizing of rubber new product, existing kind
Modification, a large amount of work has been done for the use of the research of formula.Wherein, become with the rubber particles of precrosslink and solve rubber
The modifying agent of tire " Magic triangle " problem, several big rubber companies are all carrying out the research work of this respect in the world, and obtain
Notable achievement in research.The research of country's this respect is seldom at present, and only Sinopec Beijing Chemical Research Institute, asphalt in Shenli Refinery exist
Cooperation carries out the research that the rubber particles of precrosslink are modified with tread rubber, with the poly- butylbenzene rubber of breast for having blended part precrosslinked rubber latex
Tread rubber prepared by glue SBR1502 Lab Products, rolling resistance, wet and slippery performance, wear-resisting property aspect are preferably balanced.
There has been no the open reports that precrosslinked rubber latex cohesion production in part is carried out on existing ESBR commercial plants at present.By
In the technical characteristic of precrosslinked rubber latex itself, it is difficult to compared with the mixing of the uncrosslinked latex in basis on 10,000 tons commercial plant
Realize nano level dispersion.And because precrosslinked rubber latex interface interaction, blending amount be more than 3% mixing latex its agglomerated
Journey can cause particle obviously to become smaller, be more than 10% blending amount since its particle is meticulous, post-processing production can be caused difficult.In addition,
Having blended the mixing latex of precrosslinked rubber latex can cause cohesion turbidity of wastewater significantly raised in coacervation process, and waste water COD increases.
Invention content
The technical problem to be solved by the present invention is to：Overcome the deficiencies of the prior art and provide one kind can with blending amount big, particle
Size is adjustable, agglomerates the cohesion production technology of the few parts the ESBR precrosslinked rubber latex of waste water.
The technical solution adopted by the present invention to solve the technical problems is：The cohesion of the parts the ESBR precrosslinked rubber latex produces
Technique, which is characterized in that processing step is：
1）Speed of agitator when controlling uncrosslinked latex production is 350 rpm ~ 500rpm；A part of uncrosslinked latex is added
Precrosslink, which is carried out, in the pretreating containers that speed of agitator is 100rpm ~ 300rpm obtains precrosslinked rubber latex, the temperature of precrosslink
At 40 DEG C ~ 70 DEG C, the precrosslink time is 10 min ~ 30min for control；
2）By step 1）Uncrosslinked latex obtained is mixed with precrosslinked rubber latex obtained after precrosslink in static mixer
To mixing latex, the mass ratio that precrosslinked rubber latex accounts for mixing latex is 3.5% ~ 15%；
3）Epoxy glue milk flow enters collection surface, and the speed of agitator for adjusting collection surface is 280 rpm ~ 380rpm, flocculating agent, sulfuric acid, height
It flows into collection surface to be condensed after molecule flocculating agent and the clear on-line mixing of slurry and react, mixing latex, flocculating agent, sulfuric acid, high score
Sub- flocculating agent is 100 with clear mass ratio is starched：0.008~0.013：0.9~1.4：0.073~0.092：32 ~ 38, aggregation temperature
Degree is 50 DEG C ~ 60 DEG C；
4）Cohesion gained micelle is sent to drying box after being dehydrated, washing, and after drying box is dried to water content below 0.6%, breaks
Broken, compound stalk forming.
The present invention by carrying out precrosslinked rubber latex after special pretreatment carries out that cohesion, achievement unit is blended with styrene-butadiene latex
Divide the production of precrosslinked rubber.The present invention is based on existing ESBR cohesion process, small investment, short construction period is quick.This hair
It is bright to realize that precrosslink component accounting is feasible from 3.5% ~ 15%, and rubber grain size be adjusted flexibly within the scope of 1cm ~ 3cm,
Waste water COD is agglomerated down to 500mg/L or less.By turning down rotating speed in production section precrosslinked rubber latex, uncrosslinked latex is produced
Shi Tigao rotating speeds simultaneously increase substantially the addition of acid additive in condensed system, and precrosslinked rubber latex is promoted in base with this
Dispersion in plinth latex, glue particle is too small after solving blending part precrosslinked rubber latex, and cohesion slurry is clear muddy, waste water COD
High problem.
Preferably, step 3）The size of micelle obtained by the aggregation is 1 cm ~ 3cm.The size of micelle is this hair
One of bright effect, technique of the invention realize precrosslink component accounting it is increased in the case of, still ensure the size of micelle not
Can obviously it become smaller.
Preferably, the pretreating containers are equipped with chuck, and chuck is passed through circulating hot water.The temperature of pretreating containers is logical
It crosses water-bath and maintains temperature, can ensure that the temperature in pretreating containers is more stablized, be conducive to pretreated effect.
Preferably, step 2）The precrosslinked rubber latex is measured by electromagnetic flowmeter with uncrosslinked latex and passes through screw rod
The rotational speed regulation realization of pump is proportionally added into be mixed in static mixer.Realize automatic gauge, and static mixing wherein
Space is saved in quickly mixing, improves production efficiency.
Preferably, the drying box point includes Room 1 ~ 6, and the bottom temp of hothouse controls respectively：Room 1, Room 2 are 75 DEG C
~ 95 DEG C, Room 3, Room 4 are 75 DEG C ~ 90 DEG C, and Room 5 are 70 DEG C ~ 85 DEG C, and Room 6 are 40 DEG C ~ 75 DEG C.The dry environment of drying box is to drying
Efficiency is affected, and the present invention provides preferred drying condition, good with the Technological adaptability of the present invention, can be with most fast efficiency
The dry water content required to the present invention.
Preferably, the flocculating agent is CaCl2, KCl or Na2SO4。
Preferably, the polymer coagulant is di nitrile di amine formaldehyde condensation compound or polyamine compound.
Currently preferred flocculating agent and polymer coagulant and the pretreated latex adaptability of the present invention are best, are agglomerating
During be not in that precrosslinked rubber latex is gathered, ensure that precrosslinked rubber latex adequately disperses in coacervation process.
Preferably, step 3）The mixing latex, flocculating agent, sulfuric acid, polymer coagulant are with clear mass ratio is starched
100：0.01~0.011：1.1~1.2：0.08~0.085：35~36.The amount ratio of preferred latex and auxiliary agent can reach this hair
Bright best flocculating result.
Preferably, step 4）The dehydration, washing are that micelle after aggregation and the clear mixed liquor of slurry enter first
Spiral dewatering screen is dehydrated the micelle isolated and enters washing trough washery by chute；Enter together with cleaning solution after micelle washing
Second spiral dewatering screen, micelle into extruder slough moisture after being detached with cleaning solution, by hot-air after the blob of viscose of bulk is broken
It is sent to drying box.
Compared with prior art, have possessed by a kind of cohesion production technology of parts ESBR precrosslinked rubber latex of the invention
Beneficial effect is：The present invention by carrying out precrosslinked rubber latex after special pretreatment carries out that cohesion is blended with styrene-butadiene latex, realizes
The production of part precrosslinked rubber.The present invention is based on existing SBR of emulsion polymerization（ESBR）Cohesion process, it is only necessary to increase
Part storage tank, pipeline change promoter addition, are easy to implement on current mainstream ESBR devices, small investment, construction period
It is short, it is quick.Precrosslink component can reach nano level dispersion in the compounded rubber of production, and the present invention realizes precrosslink group
Point accounting is feasible from 3.5% ~ 15%, and rubber grain size can be adjusted flexibly within the scope of 1cm ~ 3cm, cohesion waste water COD down to
500mg/L or less.Anticipating before being mixed by two kinds of latex（Rotating speed is turned down in production section precrosslinked rubber latex, is produced
Rotating speed is improved when uncrosslinked latex）And improve the dosage of sulfuric acid（The addition of acid additive increases than former dosage in condensed system
Add 10% ~ 70%）, dispersion of the precrosslinked rubber latex in base latex is promoted with this, after solving blending part precrosslinked rubber latex
The problems such as glue particle is too small, and cohesion slurry is clear muddy, and waste water COD is high.
Specific implementation mode
With reference to specific embodiment, the present invention will be further described, and wherein embodiment 1 is most preferred embodiment.
Embodiment 1
Precrosslinked rubber latex is injected in pretreating containers, and temperature is 55 DEG C, and stirring is opened, and rotating speed is 100rpm ~ 300rpm, when stirring
Between after 20min, by screw pump adjustment of rotational speed flow, mixed with uncrosslinked latex according to 5% ratio, when uncrosslinked latex production
Rotating speed be 450rpm；Latex flows into collection surface after static mixer mixes.Flocculating agent, sulfuric acid, polymer coagulant with
It starches to flow into collection surface after clear on-line mixing and agglomerate, the speed of agitator for adjusting collection surface is 320rpm, flocculating agent, sulfuric acid, high score
It flows into collection surface to be condensed after sub- flocculating agent and the clear on-line mixing of slurry and react, mixing latex, flocculating agent, sulfuric acid, macromolecule
Flocculating agent is 100 with clear mass ratio is starched：0.01：1.1：0.08：35, flocculating agent selects Na2SO4, polymer coagulant selection two
Nitrile diamines formaldehyde condensation products；Condensation temperature is 55 DEG C；Micelle enters the first spiral dewatering screen, glue with clear mixed liquor is starched through chute
Grain enters sink by chute；The mixed liquor clear with slurry enters the second spiral dewatering screen by chute after washing, is glued in sieve
Grain enters extruder from after with slurry sorting through chute；Moisture therein is sloughed under squeezing action, and helical feed is fallen into through hopper
Then machine enters after the blob of viscose of bulk is crushed by crusher through chute and falls into the stainless steel tube with venturi tube structure through chute
It is interior, micelle is sent to drying box by the hot wind of air-blaster；
Drying box is divided into Room 1 ~ 5 and cold house, and the bottom temp of each hothouse controls respectively, and Room 1 ~ 2 is 88 DEG C, and Room 3 ~ 4 are 83 DEG C,
Room 5 are 79 DEG C, and cold house is 60 DEG C.Drying box exports the water content of micelle below 0.6%；In drying box discharge chamber, rubber is picked
The thin tooth of glue machine is evacuated, and most afterwards after crusher in crushing, is fallen on and is closed on material machine, and be sent to the automatic of post-processing unit by conjunction material machine
Scale, compound stalk forming after weighing；The wet micelle sent by heating air is fallen into after cyclone separator detaches on vibration material distributor,
Micelle is evenly distributed on by vibration material distributor on the porous carrier bar of stainless steel；By adjusting vibration material distributor amplitude, swing speed
And angle, distribution of the micelle on carrier bar can be adjusted；Micelle on carrier bar in stratiform convey, hot wind under carrier bar towards
On blow over glue-line, so that glue is dried, bondline thickness can by change chain tape speed be adjusted, normal control is in 7 cm ~ 8cm.
Embodiment 2
Then precrosslinked rubber latex to be injected in pretreating containers, temperature is 50 DEG C, and stirring is opened, and rotating speed is 100rpm ~ 300rpm,
After mixing time 30min, by screw pump adjustment of rotational speed flow, mixed with uncrosslinked latex according to 8% ratio, uncrosslinked latex
Rotating speed when production is 400rpm；The condition of uncrosslinked latex is the same as original production condition.Latex flows after static mixer mixes
Enter collection surface, the speed of agitator for adjusting collection surface is 350rpm.Flocculating agent, sulfuric acid, polymer coagulant and the clear on-line mixing of slurry
It flows into collection surface and agglomerates afterwards.Condensation temperature is 52 DEG C, mixing latex, flocculating agent, sulfuric acid, the polymer coagulant matter clear with slurry
Amount is than being 100：0.011：1.2：0.085：36, flocculating agent selects CaCl2, polymer coagulant selection polyamine compound.It is dry
Dry case is divided into Room 1 ~ 5 and cold house, and the bottom temp of each hothouse controls respectively, and Room 1 ~ 2 is 90 DEG C, and Room 3 ~ 4 are 87 DEG C, and Room 5 are
82 DEG C, cold house is 55 DEG C.Drying box exports the water content of micelle 0.6%, remaining is the same as embodiment 1 below.
Embodiment 3
Then precrosslinked rubber latex to be injected in pretreating containers, temperature is 60 DEG C, and stirring is opened, and rotating speed is 100rpm ~ 300rpm,
After mixing time 20min, by screw pump adjustment of rotational speed flow, mixed with uncrosslinked latex according to 12% ratio, uncrosslinked latex
Rotating speed when production is 380rpm；The condition of uncrosslinked latex is the same as original production condition.Latex flows after static mixer mixes
Enter collection surface, the speed of agitator for adjusting collection surface is 300rpm.Flocculating agent, sulfuric acid, polymer coagulant and the clear on-line mixing of slurry
It flows into collection surface and agglomerates afterwards.Condensation temperature is 57 DEG C, mixing latex, flocculating agent, sulfuric acid, the polymer coagulant matter clear with slurry
Amount is than being 100：0.009：1.3：0.076：34, flocculating agent selects KCl, polymer coagulant to select dintrile diamines formaldehyde condensation
Object.Drying box is divided into Room 1 ~ 5 and cold house, and the bottom temp of each hothouse controls respectively, Room 1 ~ 2 be 90 DEG C, Room 3 ~ 4 be 85 DEG C, 5
Room is 75 DEG C, and cold house is 60 DEG C.Drying box exports the water content of micelle 0.6% hereinafter, remaining is the same as embodiment 1 below.
Embodiment 4
Then precrosslinked rubber latex to be injected in pretreating containers, temperature is 40 DEG C, and stirring is opened, and rotating speed is 100rpm ~ 300rpm,
After mixing time 30min, by screw pump adjustment of rotational speed flow, mixed with uncrosslinked latex according to 15% ratio, uncrosslinked latex
Rotating speed when production is 350rpm；The condition of uncrosslinked latex is the same as original production condition.Latex flows after static mixer mixes
Enter collection surface, the speed of agitator for adjusting collection surface is 280 rpm.Flocculating agent, sulfuric acid, polymer coagulant and the clear on-line mixing of slurry
It flows into collection surface and agglomerates afterwards.Condensation temperature is 50 DEG C, mixing latex, flocculating agent, sulfuric acid, the polymer coagulant matter clear with slurry
Amount is than being 100：0.008： 1.4：0.073：38, flocculating agent selects Na2SO4, polymer coagulant selection polyamine compound.It is dry
Dry case is divided into Room 1 ~ 5 and cold house, and the bottom temp of each hothouse controls respectively, and Room 1 ~ 2 is 75 DEG C, and Room 3 ~ 4 are 75 DEG C, and Room 5 are
85 DEG C, cold house is 75 DEG C.Drying box exports the water content of micelle 0.6% hereinafter, remaining is the same as embodiment 1 below.
Embodiment 5
Precrosslinked rubber latex is injected in pretreating containers, and temperature is 70 DEG C, and stirring is opened, and rotating speed is 100rpm ~ 300rpm, when stirring
Between after 10min, by screw pump adjustment of rotational speed flow, mixed with uncrosslinked latex according to 3.5% ratio, uncrosslinked latex production
When rotating speed be 500rpm；The condition of uncrosslinked latex is the same as original production condition.Latex flows into solidifying after static mixer mixes
Poly- slot.It flows into collection surface and agglomerates after flocculating agent, sulfuric acid, polymer coagulant and the clear on-line mixing of slurry, adjust stirring for collection surface
Mix rotating speed is 380rpm.Condensation temperature is 60 DEG C, mixing latex, flocculating agent, sulfuric acid, the polymer coagulant mass ratio clear with slurry
It is 100： 0.013：0.9：0.092：32, flocculating agent selects CaCl2, polymer coagulant selection di nitrile di amine formaldehyde condensation compound；
Drying box is divided into Room 1 ~ 5 and cold house, and the bottom temp of each hothouse controls respectively, and Room 1 ~ 2 is 95 DEG C, and Room 3 ~ 4 are 90 DEG C, Room 5
It it is 70 DEG C, cold house is 40 DEG C.Drying box exports the water content of micelle 0.6% hereinafter, remaining is the same as embodiment 1 below.
Comparative example 1
The rotating speed of the stirring container of precrosslinked rubber latex is 320rpm, and rotating speed when uncrosslinked latex produces is 320rpm；Remaining is same
Embodiment 1.
Comparative example 2
Brass tacks mode is with embodiment 1, the difference is that the speed of agitator of collection surface is 470rpm.
Comparative example 3
Brass tacks mode is with embodiment 1, the difference is that the dosage of sulfuric acid is reduced, mixing latex, flocculating agent, sulfuric acid, macromolecule
Flocculating agent is 100 with clear mass ratio is starched：0.01：0.6：0.08：35.
The testing result of the particle size of the gel and waste water COD of 1 embodiment and comparative example of table
。
Rubber grain made from present invention process is big as can be seen from Table 1, and particle size of the gel can press embodiment item as needed
Part is adjusted；It is low to agglomerate waste water COD.
The above described is only a preferred embodiment of the present invention, being not that the invention has other forms of limitations, appoint
What those skilled in the art changed or be modified as possibly also with the technology contents of the disclosure above equivalent variations etc.
Imitate embodiment.But it is every without departing from technical solution of the present invention content, according to the technical essence of the invention to above example institute
Any simple modification, equivalent variations and the remodeling made, still fall within the protection domain of technical solution of the present invention.
Claims (9)
1. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex, which is characterized in that processing step is：
1）Speed of agitator when controlling uncrosslinked latex production is 350 rpm ~ 500rpm；A part of uncrosslinked latex is added
Precrosslink, which is carried out, in the pretreating containers that speed of agitator is 100rpm ~ 300rpm obtains precrosslinked rubber latex, the temperature of precrosslink
At 40 DEG C ~ 70 DEG C, the precrosslink time is 10 min ~ 30min for control；
2）By step 1）Uncrosslinked latex obtained is mixed with precrosslinked rubber latex obtained after precrosslink in static mixer
To mixing latex, the mass ratio that precrosslinked rubber latex accounts for mixing latex is 3.5% ~ 15%；
3）Epoxy glue milk flow enters collection surface, and the speed of agitator for adjusting collection surface is 280 rpm ~ 380rpm, flocculating agent, sulfuric acid, height
It flows into collection surface to be condensed after molecule flocculating agent and the clear on-line mixing of slurry and react, mixing latex, flocculating agent, sulfuric acid, high score
Sub- flocculating agent is 100 with clear mass ratio is starched：0.008~0.013：0.9~1.4：0.073~0.092：32 ~ 38, aggregation temperature
Degree is 50 DEG C ~ 60 DEG C；
4）Cohesion gained micelle is sent to drying box after being dehydrated, washing, and after drying box is dried to water content below 0.6%, breaks
Broken, compound stalk forming.
2. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：Step
3）The size of micelle obtained by the aggregation is 1 cm ~ 3cm.
3. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：It is described
Pretreating containers be equipped with chuck, chuck is passed through circulating hot water.
4. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：Step
2）The precrosslinked rubber latex is measured by electromagnetic flowmeter with uncrosslinked latex and is pressed by the realization of the rotational speed regulation of screw pump
Ratio is added to be mixed in static mixer.
5. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：It is described
Drying box point include Room 1 ~ 6, the bottom temp of hothouse controls respectively：Room 1, Room 2 are 75 DEG C ~ 95 DEG C, and Room 3, Room 4 are 75 DEG C
~ 90 DEG C, Room 5 are 70 DEG C ~ 85 DEG C, and Room 6 are 40 DEG C ~ 75 DEG C.
6. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：It is described
Flocculating agent be CaCl2, KCl or Na2SO4。
7. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：It is described
Polymer coagulant be di nitrile di amine formaldehyde condensation compound or polyamine compound.
8. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：Step
3）Mixing latex, flocculating agent, sulfuric acid, polymer coagulant and the clear mass ratio of slurry is 100：0.01~0.011：1.1~
1.2：0.08~0.085：35~36.
9. a kind of cohesion production technology of parts ESBR precrosslinked rubber latex according to claim 1, it is characterised in that：Step
4）The dehydration, washing are that micelle after aggregation and the clear mixed liquor of slurry enter the first spiral dewatering screen, dehydration separation
The micelle gone out enters washing trough washery by chute；Enter the second spiral dewatering screen, micelle together with cleaning solution after micelle washing
Moisture is sloughed into extruder, drying box is sent to by hot-air after the blob of viscose of bulk is broken after being detached with cleaning solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710050902.XA CN108341895B (en) | 2017-01-23 | 2017-01-23 | Coagulation production process of ESBR (ethylene styrene-butadiene rubber) partially pre-crosslinked latex |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710050902.XA CN108341895B (en) | 2017-01-23 | 2017-01-23 | Coagulation production process of ESBR (ethylene styrene-butadiene rubber) partially pre-crosslinked latex |
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| CN108341895B CN108341895B (en) | 2020-10-27 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102428125A (en) * | 2009-03-17 | 2012-04-25 | 塞姆普雷特控股股份公司 | Method for producing a cross-linked elastomer |
| CN102617901A (en) * | 2012-03-22 | 2012-08-01 | 北京化工大学 | Application of hydrogenated nitrile latex |
| US20150141576A1 (en) * | 2013-11-20 | 2015-05-21 | Zeon Chemicals L.P. | Process for producing coalesced rubber microparticles and their blends with epoxy resins |
| CN105778165A (en) * | 2014-12-16 | 2016-07-20 | 北京橡胶工业研究设计院 | Natural rubber/radiation-crosslinked nitrile-butadiene rubber composite material and preparation method therefor |
-
2017
- 2017-01-23 CN CN201710050902.XA patent/CN108341895B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102428125A (en) * | 2009-03-17 | 2012-04-25 | 塞姆普雷特控股股份公司 | Method for producing a cross-linked elastomer |
| CN102617901A (en) * | 2012-03-22 | 2012-08-01 | 北京化工大学 | Application of hydrogenated nitrile latex |
| US20150141576A1 (en) * | 2013-11-20 | 2015-05-21 | Zeon Chemicals L.P. | Process for producing coalesced rubber microparticles and their blends with epoxy resins |
| CN105778165A (en) * | 2014-12-16 | 2016-07-20 | 北京橡胶工业研究设计院 | Natural rubber/radiation-crosslinked nitrile-butadiene rubber composite material and preparation method therefor |
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