TH57776A - Removal of volatile organic compounds in continuous slurry polymerization. - Google Patents

Abstract

DC60 (30/11/44) The process/machinery was revealed for the continuous separation of a liquid medium comprising a diluent and an inert monomer from the discharge product of a polymer synthesis product comprising a diluent and an inert monomer and a solid polymer comprising a discharge product of a polymer synthesis product continuously from a cyclic reactor through a discharge valve and transfer pipe into a medium-pressure instantaneous vaporization tank, tank one, with a conical bottom bounded by a significantly straight side tilted at an angle to the horizontal equal to or greater than the angle of the slurry/solid polymer slide and an outlet sealing chamber of diameter (d) and length (I) to maintain the required volume of the concentrated solid polymer/slurry in the outlet sealing chamber, e.g., to achieve pressure sealing while continuously dischargeing the bottom product with a push flow of the concentrated solid polymer/slurry from the instantaneous vaporization tank, tank one. The sealing chamber at the outlet, through a attenuator at the outlet of the sealing chamber, has an inclined side defined by a significantly straight side inclined at an angle to the horizontal equal to or greater than the angle of the slurry/solid polymer slide remaining after the removal of approximately 50 to 100% of the diluent, to a second instantaneous vaporization tank at a lower pressure. The process/machinery was revealed for the continuous separation of the liquid hollow body comprising the diluent and the non-reactive monomer from the discharge material of the polymer synthesis, comprising the diluent, non-reactive monomer, and the solid polymer, with the discharge material of the polymer synthesis continuing from the cyclic reactor through a discharge valve and transfer pipe into the first medium-pressure instantaneous vaporization tank, with a conical bottom defined by a significantly straight side inclined at an angle to the horizontal equal to or greater than the angle of the slurry/solid polymer slide. and a sealing chamber at the outlet with diameter (d) and length (I) to maintain the desired volume of the concentrated solid polymer/slurry in the sealing chamber at the outlet, for example, to achieve pressure sealing while continuously releasing the bottom product with a push flow of the concentrated solid polymer/slurry from the first instantaneous vaporization tank from the sealing chamber at the outlet through an outlet reducer with a slanted side determined by a significantly straight side slanted at an angle to the horizontal equal to or greater than the angle of slide of the remaining solid polymer after removal of approximately 50 to 100% of the diluent into the second instantaneous vaporization tank at a lower pressure.

Claims (54)

1. The process for polymer production in a continuous slurry cycle reactor consists of: - Reaction of monomers in a hydrocarbon diluent to form slurry of the polymerization of the solid polymer in a liquid medium; - Discharge of the polymerization slurry, which consists of the discharged solid polymer slurry in the discharged liquid medium, through a discharge opening into the first transfer pipe; - Heating of the discharged material with the first heater; - Rapid vaporization of the discharged material in the first rapid vaporization tank, where at least one portion of the liquid medium is vaporized to form the first rapid vaporization vapor and first rapid vaporization slurry; - Condensation of at least one portion of the first rapid vaporization vapor without compression; - Discharge of the first rapid vaporization slurry into the second transfer pipe; - Heating of the first rapid vaporization slurry with a heater. The second heating element and - the slurry is instantly vaporized from the first instantaneous vaporization to the second instantaneous vaporization. 2. The process under claim 1, in which the process is further incorporated - the vaporization of the slurry from the first instantaneous vaporization to form the second instantaneous vaporization and the second instantaneous solid polymer, in which at least one part of the liquid from the first instantaneous vaporization is vaporized immediately on the second instantaneous vaporization. 3. The process under claim 2 which includes the condensation of vapor from the second immediate vaporization, at least one part from the second immediate vaporization. 4. The process under claim 1 in which approximately 50% to approximately 100% of the liquid medium in the released substance is vaporized by a first instantaneous vaporization. 5. The process under claim 2 in which approximately 50% to approximately 100% of the liquid medium in the released substance is vaporized by one instantaneous vaporization. 6. The process under claim 3 in which approximately 50% to approximately 100% of the liquid medium in the released substance is vaporized by one instantaneous vaporization. 7. The process under claim 1 in which approximately 75% to approximately 100% of the liquid medium in the released substance is vaporized by one instantaneous vaporization. 8. The process under claim 2 in which approximately 75% to approximately 100% of the liquid medium in the released substance is vaporized by one instantaneous vaporization. 9. The process under claim 3 in which approximately 75% to approximately 100% of the liquid medium in the released substance is vaporized by one instantaneous vaporization. 10. The process under claim 1 in which approximately 95% to approximately 100% of the liquid medium in the released substance is vaporized from one instantaneous vaporization to the next. 11. The process under claim 2 in which approximately 95% to approximately 100% of the liquid medium in the released substance is vaporized from one instantaneous vaporization to the first instantaneous vaporization. 12. The process under claim 3 in which approximately 95% to approximately 100% of the liquid medium in the released substance is vaporized from one instantaneous vaporization to the next. 13. The process under claim 2 in which approximately 50% to 100% of the liquid medium from the first instantaneous vaporization is vaporized further by the second instantaneous vaporization. 14. The process under claim 3 in which approximately 50% to 100% of the liquid medium from the first instantaneous vaporization is vaporized further from the second instantaneous vaporization. 15. The process under claim 2 in which at least approximately 75% of the liquid medium from the first instantaneous vaporization is vaporized from the second instantaneous vaporization. 16. The process under claim 3 in which at least approximately 75% of the liquid medium from the first instantaneous vaporization is vaporized from the second instantaneous vaporization. 17. The process under claim 2 in which at least approximately 95% of the liquid medium from the first instantaneous vaporization is vaporized from the second instantaneous vaporization. 18. The process under claim 3 in which at least approximately 95% of the liquid medium from the first instantaneous vaporization is vaporized from the second instantaneous vaporization. 19. The process under claim 1 where the reactor is operated at approximately 150 to 250 °F. 20. The process pursuant to claim 19, where the reactor is operated at approximately 175 to 230°F. 21. The process pursuant to claim 20, where the reactor is operated at approximately 200 to 230°F. 22. The process under claim 1 where the reactor is operated at approximately 400 to 660 absolute pounds per square inch. 23. The process pursuant to claim 22, where the reactor is operated at approximately 500 to 600 absolute pounds per square inch. 24. The process pursuant to claim 23, where the reactor is operated at approximately 565 absolute pounds per square inch. 25. The process under claim 1 where the discharge of the substance into the first transfer pipe is continuous. 26. The process under claim 2 where the discharge of the substance into the first transfer pipe is continuous. 27. The process under claim 1 where the first heater is a heat exchanger on the production line. 28. The process under claim 2 where the first heater is a production line heat exchanger. 29. The process under claim 1 in which the first heater heats the released substance to a temperature below the melting temperature of the polymer. 30. The process under claim 2 in which the first heater heats the released substance to a temperature below the melting temperature of the polymer. 31. The process pursuant to claim 1 where the first instantaneous vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 32. The process pursuant to claim 2, where the first immediate vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 33. The process pursuant to claim 3, where the first instantaneous vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 34. The process pursuant to claim 4, where the first instantaneous vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 35. The process pursuant to claim 7, where the first instantaneous vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 36. The process pursuant to claim 10, where the first instantaneous vaporization is performed at approximately 140 to 315 absolute pounds per square inch. 37. The process pursuant to claim 1, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 38. The process pursuant to claim 2, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 39. The process pursuant to claim 3, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 40. The process pursuant to claim 4, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 41. The process pursuant to claim 7, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 42. The process pursuant to claim 10, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 43. The process pursuant to claim 31, where a second immediate vaporization is performed at approximately 15 to 100 absolute pounds per square inch. 44. The process under claim 1 in which the heat applied to the first and second heaters is adjusted according to at least one process parameter. 45. The process under claim 2 in which the heat applied to the first and second heaters is adjusted to at least one process parameter. 46. The process under claim 3 in which the heat applied to the first and second heaters is adjusted according to at least one process parameter. 47. The process under claim 4 in which the heat applied to the first and second heaters is adjusted according to at least one process parameter. 48. The process pursuant to claim 44 in which the heat applied to the heaters along the production line is adjusted in a manner that significantly reduces equipment clogging. 49. The process pursuant to claim 47 in which the heat applied to the heaters along the production line is adjusted in a manner that significantly reduces equipment clogging. 50. The process pursuant to claim paragraph 44 in which the heat applied to the heaters along the production line is adjusted in a manner to improve the drying of the polymer product. 51. The process pursuant to claim 47 in which the heat applied to the heating elements along the production line is adjusted in a manner to improve the drying of the polymer product. 52. The process pursuant to claim 44 in which the heat applied to the heaters along the production line is adjusted in a manner to improve the recovery of the diluent. 53. The process pursuant to claim 47 in which the heat applied to the heaters along the production line is adjusted in a manner to improve the recovery of the diluent. 54. The process for polymer production in a continuous slurry cycle reactor consists of: - Reaction of monomers in a hydrocarbon diluent to form slurry of the polymerization of the solid polymer in a liquid medium; - Discharge of the polymerization slurry, which consists of the discharged solid polymer slurry in the discharged liquid medium, through a discharge opening into the first transfer pipe; - Heating of the discharged material with the first heater; - Rapid vaporization of the discharged material in the first rapid vaporization tank, where at least one portion of the liquid medium is vaporized to form the first rapid vaporization vapor and first rapid vaporization slurry; - Condensation of at least one portion of the first rapid vaporization vapor without compression; - Discharge of the first rapid vaporization slurry into the second transfer pipe; - Heating of the first rapid vaporization slurry with a heater. Second heating – vaporizing the slurry from the first instantaneous vaporization to the second instantaneous vaporization for reformation and solid polymerization from the second instantaneous vaporization, and – condensing at least one-third of the vapor from the second instantaneous vaporization, where – approximately 50 to 100% of the liquid medium in the discharged substance is vaporized from the first instantaneous vaporization – at least 50% of the liquid from the first instantaneous vaporization is vaporized from the second instantaneous vaporization – the reactor was operated at approximately 175 to 230°F – the reactor was operated at approximately 500 to 600 absolute pounds per square inch – the second instantaneous vaporization was operated at approximately 15 to 100 absolute pounds per square inch, and – the heat input to the inline heaters was adjusted in a manner to significantly minimize equipment clogging.