CN1187503A - Process for devolatilization of copolymer containing styrene-maleic acid anhydride copolymer - Google Patents
Process for devolatilization of copolymer containing styrene-maleic acid anhydride copolymer Download PDFInfo
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- CN1187503A CN1187503A CN97106214A CN97106214A CN1187503A CN 1187503 A CN1187503 A CN 1187503A CN 97106214 A CN97106214 A CN 97106214A CN 97106214 A CN97106214 A CN 97106214A CN 1187503 A CN1187503 A CN 1187503A
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- devolatilization
- styrene
- anhydride copolymer
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- maleic anhydride
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Abstract
A devolatilizing process for styrene-maleic acid anhydride copolymer features that a twin-screw extruder with 3-5 exhaust ports is used and regulating the temp and pressure of each exhaust port to well match the vacuum level of exhaust port and material temp at correspondent port so as to make the content of residual monomer in resin less than 1000 PPm. Its advantages are use of raw material with high content of residual monomer and full of devolatilization.
Description
The present invention relates to contain the process for devolatilization of styrene-maleic anhydride copolymer, particularly about technology with the twin screw extruder devolatilization.
Styrene-maleic anhydride copolymer (being called for short SMA), it is to close reaction by vinylbenzene and maleic anhydride by bulk copolymerization to get.In reaction process, if the styrene monomer conversion rate surpasses 90%, the copolymer resins that then can not obtain having good transparency and thermostability, and during monomer conversion less than 40%, residual more monomer in the polymerization system is handled devolatilization and the solvent recuperation engineering contradiction that over-burden thereby cause.Industrial for this reason normal control styrene monomer conversion rate is greater than 60%, even like this, also has 40% styrene monomer residual in the system, must remove and reclaim by devolatilization.
The polymer of the phenylethylene that solution polymerization in the past or mass polymerization obtain, will be to remove monomer or volatile matter in the polymerization system, the heat exchanger of most employing heating tubular types is also removed monomer methods under certain vacuum tightness, for example the document special permission discloses the method that proposes to adopt bar formula book film evaporator and the coupling of versatility vented extruder among the flat 3-73570, the bar formula that falls book film evaporator can remove the unreacted monomer of high deal in the system, the versatility vented extruder can further be removed monomer residual in the system, but this method exists energy consumption big, the shortcoming that Production Flow Chart is long.Introduced the devolatilization technology of horizontal-type biaxial screw devolatilizer in the document US 2931793, but the devolatilization ability of this technology is lower, it requires, and monomer residue content must be lower than 35% in the system, and finally the resin residue amount of monomer reaches 0.5%, is difficult to adapt to the devolatilization requirement of high residue amount of monomer.
In order to overcome the shortcoming that above document exists, the purpose of this invention is to provide a kind of process for devolatilization that contains styrene-maleic anhydride copolymer, in this technology in the permission system levels of residual monomers reach 36～60%, and after the final devolatilization in the system monomeric residual quantity be lower than 1000PPm.
The objective of the invention is to realize: a kind of process for devolatilization that contains styrene-maleic anhydride copolymer by following technical scheme, comprise styrene-maleic anhydride copolymer, styrene monomer in the material solution, employing has the twin screw extruder devolatilization of 3～5 venting ports, the 1st of twin screw extruder, 2 exhaust port pressure are-0.02～-0.040MPa, temperature is 120～150 ℃; The 3rd exhaust port pressure is-0.040～-0.080MPa, temperature is 160～190 ℃; The 4th, 5 exhaust port pressure is-0.080～-0.098MPa, temperature is 210～240 ℃.
In the technique scheme, the residual quantity of styrene monomer can reach 36～60% (weight) in the raw material, and the 1st, 2 venting port can be merged into a venting port after the parallel connection, and the 4th, 5 venting port can be merged into a venting port.
In this process for devolatilization, because we have adopted the twin shaft screw rod devolatilization forcing machine with a plurality of venting ports and the combination of extraordinary threaded block, regulate the temperature and the pressure of each venting port, make the vacuum tightness of venting port good coupling arranged with the temperature of charge of corresponding mouth, thereby the copolymerization system that contains the high-phenylethylene residual monomer is separated quickly and easily, and residual monomer content is lower than 1000PPm in the final gained resin, this method technical process is short, handle the residual monomer content height in the raw material, devolatilization is more complete, has obtained good effect.
Fig. 1 is the big exhaust magnitude of a twin screw extruder structure sketch.
1 is well heater among Fig. 1, and 2 is head, and 3 is the III venting port, 4 is screw rod, and 5 is the II venting port, and 6 is cylindrical shell, 7 is the I venting port, and 8 is single screw rod feeding machine, and 9 is hopper, 10 is the cycloidal-pin wheel speed reduction unit, and 11 is motor, and 12 is the twin screw transmission case, 13 is step-down gear, 14 is belt pulley, and 15 is motor, and 16 is support.
Raw material adds the transmission through screw rod from hopper 9, through first, second, third ... venting port removes residual monomer, thereby makes the polymkeric substance of acquisition reach requirement.[embodiment 1]
Percent polymerization is 55% phenylethylene-maleic anhydride copolymerization system, enter syllogic twin screw devolatilization forcing machine with 4 kilograms/hour speed, temperature at first venting port is 140 ℃, vacuum tightness is 20KPa, the temperature of second venting port is 180 ℃, and vacuum tightness is 40KPa, and the temperature of the 3rd venting port is 230 ℃, vacuum tightness is under the operational condition of 95KPa, obtains that the styrene monomer residual content is 0.099% in the styrene-maleic anhydride copolymer.[embodiment 2]
The styrene solution that contains multipolymer 60% (weight), enter syllogic twin screw devolatilization forcing machine with 5 kilograms/hour speed, 150 ℃ of the first venting port temperature, vacuum tightness 30KPa, the second venting port temperature is 190 ℃, vacuum tightness 60KPa, and the 3rd venting port temperature is 240 ℃, under the operational condition of vacuum tightness 98KPa, obtain styrene monomer residual content 0.080% (weight) in the styrene-maleic anhydride copolymer.[embodiment 3]
The styrene solution that contains multipolymer 50% (weight), enter syllogic twin screw devolatilization forcing machine with 3 kilograms/hour speed, 120 ℃ of the first venting port temperature, vacuum tightness 30KPa, the second venting port temperature is 160 ℃, and vacuum tightness is 80KPa, and the 3rd venting port temperature is 210 ℃, vacuum tightness is under the operational condition of 90KPa, obtains styrene monomer residual content 0.095% (weight) in the styrene-maleic anhydride copolymer.[embodiment 4]
The styrene solution that contains multipolymer 64% (weight), enter five-part form twin screw devolatilization forcing machine with 2 kilograms/hour speed, the first venting port temperature is 140 ℃, vacuum tightness 20KPa, the second venting port temperature is 150 ℃, vacuum tightness 30KPa, the 3rd venting port temperature is 180 ℃, vacuum tightness 40KPa, the 4th venting port temperature is 210 ℃, and vacuum tightness is 80KPa, and the 5th venting port temperature is 240 ℃, vacuum tightness is under the operational condition of 88KPa, obtains styrene monomer residual content 0.044% (weight) in the styrene-maleic anhydride copolymer.[embodiment 5]
The styrene solution that contains multipolymer 40% (weight), enter five-part form twin screw devolatilization forcing machine with 2 kilograms/hour speed, the first venting port temperature is 140 ℃, vacuum tightness 30KPa, the second venting port temperature is 150 ℃, vacuum tightness 40KPa, the 3rd venting port temperature is 190 ℃, vacuum tightness 80KPa, the 4th venting port temperature is 230 ℃, and vacuum tightness is 90KPa, and the 5th venting port temperature is 240 ℃, vacuum tightness is under the operational condition of 98KPa, obtains styrene monomer residual content 0.056% (weight) in the styrene-maleic anhydride copolymer.
Claims (4)
1, a kind of process for devolatilization that contains styrene-maleic anhydride copolymer, comprise styrene-maleic anhydride copolymer, styrene monomer in the material solution, it is characterized in that with twin shaft screw extrusion press devolatilization with 3～5 venting ports, the 1st of twin screw extruder, 2 exhaust port pressure are-0.020～-0.040MPa, temperature is 120～150 ℃; The 3rd exhaust port pressure is-0.040～-0.080MPa, temperature is 160～190 ℃; The 4th, 5 exhaust port pressure is-0.080～-0.098MPa, temperature is 210～240 ℃.
2, according to the described process for devolatilization that contains styrene-maleic anhydride copolymer of claim 1, it is characterized in that containing in the material solution styrene monomer residual content is 36～60% (weight).
3,, it is characterized in that the 1st, 2 venting port can merge into a venting port after the parallel connection according to the described process for devolatilization that contains styrene-maleic anhydride copolymer of claim 1.
4,, it is characterized in that the 4th, 5 venting port can merge into a venting port after the parallel connection according to the described process for devolatilization that contains styrene-maleic anhydride copolymer of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106214A CN1056623C (en) | 1997-01-10 | 1997-01-10 | Process for devolatilization of copolymer containing styrene-maleic acid anhydride copolymer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106214A CN1056623C (en) | 1997-01-10 | 1997-01-10 | Process for devolatilization of copolymer containing styrene-maleic acid anhydride copolymer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1187503A true CN1187503A (en) | 1998-07-15 |
| CN1056623C CN1056623C (en) | 2000-09-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97106214A Expired - Fee Related CN1056623C (en) | 1997-01-10 | 1997-01-10 | Process for devolatilization of copolymer containing styrene-maleic acid anhydride copolymer |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI561540B (en) * | 2014-09-09 | 2016-12-11 | Asahi Kasei Chemicals Corp |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06827B2 (en) * | 1985-04-01 | 1994-01-05 | 三井東圧化学株式会社 | Continuous treatment method for polymerization reaction mixture |
| JPH0662694B2 (en) * | 1991-04-04 | 1994-08-17 | 旭化成工業株式会社 | Method for producing copolymer having excellent heat resistance |
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1997
- 1997-01-10 CN CN97106214A patent/CN1056623C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI561540B (en) * | 2014-09-09 | 2016-12-11 | Asahi Kasei Chemicals Corp |
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| CN1056623C (en) | 2000-09-20 |
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Granted publication date: 20000920 Termination date: 20100210 |