Process for the production of water and solvent-free nitrile rubbers

Patent metadata

Field	Value
Publication number	US-9469697-B2
Application number	US-201113635810-A
Country	US
Kind code	B2
Filing date	Mar 21, 2011
Priority date	Mar 25, 2010
Publication date	Oct 18, 2016
Grant date	Oct 18, 2016

Abstract

The present invention relates to specific water and solvent-free nitrile rubbers having specific functional groups and/or end groups, a process for the production thereof and the use thereof. This process involves removing volatile compounds from a fluid (F) containing (1) at least one nitrile rubber and (2) at least one volatile compound, wherein the process comprises at least the steps of a.) treating the fluid (F) in at least one conversation unit, b.) retreating the concentrated fluid from step a.) in at least one retreating unit and c.) feeding the retreated concentrated fluid from step b.) into at least one retreating unit.

First claim

The invention claimed is:

1. A process of removing volatile compounds from a fluid (F) containing at least one nitrile rubber and volatile compounds, wherein the volatile compounds include water and volatile organic compounds, and wherein the process comprises:
a) treating the fluid (F) in at least one concentrator unit comprising a heater, a degassing vessel and a first vapor line, whereby the treating comprises heating the fluid (F) in the heater to produce heated fluid (G), feeding the heated fluid (G) into degassing vessel, and degassing the heated fluid (G) and removing part of the volatile compounds via the first vapor line to obtain a concentrated fluid (H),
b) reheating the concentrated fluid (H) from step a) in at least one reheating unit to obtain a reheated concentrated fluid (L); and
c) feeding the reheated concentrated fluid (L) from step b) into at least one extruder unit comprising at least an extruder degassing section comprising a conveying section, a vent port with one or more second vapor lines, accumulating sections and an outlet section, and removing the volatile compounds through the vent ports and second vapor lines; whereby the reheated concentrated fluid (L) is free-flowing upon entering the extruder degassing section and the nitrile rubber obtained at the outlet section is substantially free of the volatile compounds,
and wherein the nitrile rubber comprises
(i) repeating units derived from at least one conjugated diene, at least one α,β-unsaturated nitrile and optionally one or more copolymerizable monomers and
(ii) one or more structural element of the general formulae (I), (II), (III), (IV) or (V)

wherein:
Z represents H, branched or unbranched, saturated or one or more times unsaturated alkyl, saturated or one or more times unsaturated carbo- or hetercyclic residue, aryl, heteroaryl, arylalkyl, heteroarylalkyl, alkoxy, aryloxy, heteroaryloxy, amino, amide, hydroxyimino, carbamoyl, akoxycarbonyl, F, Cl, Br, I, hydroxy, phosphonato, phosphinato, alkylthio, arylthio, sulfanyl, thiocarboxy, sulfono, sulfino, sulfeno, sulfonyl, sulfamoyl, silyl, silyloxy, nitril, carbonyl, carboxy, oxycarbonyl, oxysulfonyl, oxo, thioxo, borate, selenate, epoxy, cyanate, thiocyanate, isocyanate, thioisocyanate and isocyanide,
M represents repeating units derived from one or more monomers which are one or more times unsaturated, including conjugated or unconjugated dienes, alkynes and vinyl compounds, or a structural element derived from polymers comprising polyether, and polyalkylenoxides, polysiloxanes, polyols, polycarbonates, polyurethanes, polyisocyanates, polysaccharides, polyester and polyamides,
n and m are same or different and are 0 to 10,000,
t is 0 or 1, if n=0, and equals 1, if n≠0,
X represents C(Z 2 ), N(Z), P(Z), P(═O)(Z), S, S(═O) or S(═O) 2 wherein Z has the same meaning as defined hereinabove,
R (a) in case that m≠0 has the same meaning as the residue Z,
(b) in case that m=0, represents H, a branched or unbranched, saturated, one or more times unsaturated alkyl, a saturated, one or more times unsaturated carbo- or heterocyclic residue, aryl, heteroaryl, arylalkyl, heteroarylalkyl, alkoxy, aryloxy, heteroaryloxy, amino, amido, carbamoyl, alkoxy, aryloxy, alkylthio, arylthio, sulfanyl, thiocarbonyl, sulfinyl, sulfono, sulfino, sulfena, sulfonyl, sulfamoyl, carbonyl, carboxy, oxycarbonyl, oxysulfonyl, axe, thioxo, epoxy, cyanate, thiocyanate, isocyanate, thioisocyanate or isocyanide.

2. The process pursuant to claim 1 , wherein the reheated concentrated fluid (L) has a viscosity of 50 to 50,000,000 MPa*s.

3. The process pursuant to claim 1 , wherein a content of the volatile compounds in the nitrile rubber obtained at the outlet is less than 1.25 wt % based on the mass of the nitrile rubber.

4. The process pursuant to claim 1 , wherein the fluid (F) contains 3 to 50 wt % of the non-volatile nitrile rubber polymer and 50 to 97 wt % of the volatile compounds, whereby the aforementioned components add up to 90 to 100 wt % of the total mass of fluid (F).

5. The process pursuant to claim 1 , wherein the fluid (F) entering the heater has a temperature of 10° C. to 100° C.

6. The process pursuant to claim 1 , wherein the fluid (F) entering the heater has a viscosity of 100 mPa*s to 25,000 mPa*s.

7. The process pursuant to claim 1 , wherein the heated fluid (G) has a temperature of 100° C. to 200° C.

8. The process pursuant to claim 1 , wherein the pressure in the degassing vessel is 100 hPa to 4,000 hPa.

9. The process pursuant to claim 1 , wherein the degassing vessel is designed in the shape of a cyclone and has at least a torispherical shaped bottom to facilitate removal of concentrated fluid (H).

10. The process pursuant to claim 1 , wherein the temperature of the concentrated fluid (H) is lower than that of heated fluid (G) and is 15° C. to 100° C.

11. The process pursuant to claim 1 , wherein the temperature of the reheated concentrated fluid (L) is higher than that at the concentrated fluid (H) and is 50° C. to 200° C.

12. The process pursuant to claim 1 , wherein the extruder unit comprises an extruder selected from the group consisting of single and multiscrew extruders.

13. The process pursuant to claim 1 , wherein the extruder unit comprises means to operate separate zones of the extruder independently of each other at different temperatures so that the zones can independently be either heated, unheated or cooled.

14. The process pursuant to claim 1 , wherein the vent ports ( 15 ) comprise means to prevent the reheated concentrated fluid (L) or nitrile rubber, from coming out of the vent ports.

15. The process pursuant to claim 1 , wherein the accumulation in the accumulating sections is accomplished by kneading or throttling elements, blister discs or die plates.

16. The process pursuant to claim 1 , wherein the extruder unit comprises 1 to 30 conveying and accumulating sections.

17. The process pursuant to claim 1 , wherein the outlet section comprises means to allow the nitrile rubber product to exit the extruder, and product processing equipment, whereby the processing equipment is selected from the group consisting of combinations of die plates and cutters, combinations of die plates and underwater-pelletizing means, means for crumb formation, turbulators, and fixed knives placed at the end plate of the extruder.

18. The process pursuant to claim 1 , wherein the outlet section further comprises cooling means, whereby the cooling means are selected from the group consisting of pneumatic crumb conveyers with convective air cooling, vibrating crumb conveyers with convective air cooling, vibrating crumb conveyer with cooled contact surfaces, belt conveyers with convective air cooling, belt conveyer with cooled belts, water spraying on hot crumbs upon outlet of the extruder and underwater-pelletizing means.

19. The process pursuant to claim 1 , wherein the outlet section further comprises cooling means selected from the group consisting of heat exchangers, belt conveyors with convective air cooling, belt conveyors with cooled belts, water spraying on hot hydrogenated nitrile rubber or a water bath, whereby water serves as the coolant.

20. The process pursuant to claim 1 , further comprising adding a stripping agent in the extruder unit.

21. The process pursuant to claim 1 , further comprising adding additives

Assignees

• Paul Hanns-Ingolf
• Wagner Paul
• Feller Rolf
• Kirchhoff Jörg
• Lovegrove John
• Forner Florian
• Klimpel Michael
• Weuta Peter
• Brandau Sven
• Lanxess Deutschland Gmbh
• Arlanxeo Switzerland S A

Inventors

• Paul Hanns-Ingolf
• Wagner Paul
• Feller Rolf
• Kirchhoff Jörg
• Lovegrove John
• Forner Florian
• Klimpel Michael
• Weuta Peter
• Brandau Sven

Classifications

• C08C2/02 Primary

  Purification · CPC title

• C08C2/00

  Treatment of rubber solutions · CPC title

• C08L9/02

  Copolymers with acrylonitrile · CPC title

• C08C1/12 Primary

  by evaporation · CPC title

• C08F6/10

  Removal of volatile materials, e.g. solvents {(C08F6/001, C08F6/003, C08F6/005, C08F6/006, C08F6/008, C08F6/02, C08F6/04 take precedence)} · CPC title