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The invention is directed to polyester processes that utilizes a pipe reactor in the esterification, polycondensation, or both esterification and polycondensation processes. Pipe reactor processes of the present invention have a multitude of advantages over prior art processes including improved hea

The invention is directed to polyester processes that utilizes a pipe reactor in the esterification, polycondensation, or both esterification and polycondensation processes. Pipe reactor processes of the present invention have a multitude of advantages over prior art processes including improved heat transfer, volume control, agitation and disengagement functions.

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1. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface, the esterification pipe reactor comprising a substantially empty pipe; wherein the esterification pipe reactor is op

1. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface, the esterification pipe reactor comprising a substantially empty pipe; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a polycondensation pipe reactor formed separately of the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface, the polycondensation pipe reactor comprising a substantially empty pipe; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondition reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 2. The process of claim 1, wherein the reactants comprise terephthalic acid or dimethylterephthalate.3. The process of claim 2, wherein the polyester polymer is PET or PETG.4. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid, wherein the reactants comprise terephthalic acid or dimethylterephthalate; (c) providing a polycondensation pipe reactor formed separately of the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 5. The process of claim 4, wherein the polyester polymer is PET or PETG.6. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a polycondensation pipe reactor formed separately of the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondition reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 7. The process of claim 6, wherein the reactants do not comprise an anhydride.8. The process of claim 6, further comprising at least one weir attached to the interior surface of the esterification pipe reactor and wherein the esterification fluids flow over the weir.9. The process of claim 6, wherein the polycondensation pipe reactor further comprises at least one weir attached to the inside surface thereof and wherein the polycondensation fluids flow over the weir.10. The process of claim 9, further comprising at least one polycondensation fluid flowing through a flow inverter, wherein the flow inverter is proximate to and downstream of the weir.11. The process of claim 6, further comprising recirculating a portion of the process fluids and directing the recirculation effluent back to and therethrough the esterification reactor.12. The process of claim 6, further comprising removing vapors from the esterification pipe reactor intermediate its inlet and its outlet and/or proximate its outlet through a vent comprising substantially empty pipe.13. The process of claim 6, further comprising removing vapors from the polycondensation pipe reactor intermediate its inlet and its outlet and/or proximate its inlet or outlet through a vent comprising substantially empty pipe.14. The process of claim 12 or 13, wherein the vent further comprises an upstanding degas stand pipe coupled to the vent, wherein the degas stand pipe has a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the inlet end; and wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at an angle relative to the first section in plan view, and a third section coupled to the second section and oriented at a complimentary angle relative to the second section in plan view so that the third section is oriented substantially horizontally.15. The process of claim 14, wherein the first section is oriented at about from a 10 to about an 80 degree angle relative to the first section, and the third section is oriented at from about an 80 to about a 10 degree angle relative to the second section.16. The process of claim 14, wherein the first section is oriented at about a 45 degree angle relative to the first section, and the third section is oriented at about a 45 degree angle relative to the second section.17. The process of claim 6, wherein the esterification pipe reactor inlet is positioned at least 20 vertical feet below the esterification pipe reactor outlet.18. The process of claim 17, wherein the inlet is positioned at least 50 vertical feet below the outlet.19. The process of claim 17, wherein the inlet is positioned at least 100 vertical feet below the outlet.20. The process of claim 17, wherein the inlet is positioned from 50 to 200 vertical feet below the outlet.21. The process of claim 17, wherein the inlet is positioned from 90 to 150 vertical feet below the outlet.22. The process of claim 6, wherein the esterification pipe reactor is disposed in a substantially vertical orientation, such that the inlet is disposed vertically below the outlet, and the reactants and polyester monomer flow in an upward direction within the pipe reactor.23. The process of claim 6, wherein the esterification pipe reactor is disposed in a substantially horizontal orientation.24. The process of claim 6, wherein the polycondensation pipe reactor is substantially horizontally oriented.25. The process of claim 6, wherein the fluids present in the esterification pipe reactor are in a bubble or froth flow regime.26. The process of claim 6, wherein the fluids present in the polycondensation pipe reactor are in a stratified flow regime.27. The process of claim 6, wherein the esterification pipe reactor and polycondensation pipe reactor each have alternating linear and non-linear sections extending in their respective lengthwise direction between the respective inlets and outlets thereof.28. The process of claim 6, further comprising a seal leg positioned between and in fluid communication with the esterification process and the polycondensation process for controlling the pressure between the esterification and polycondensation processes.29. The process of claim 6, wherein the polycondensation reactor includes at least two different sections in fluid communication with one another, each section being of a different fluid pressure, and wherein a seal leg is positioned between and in fluid communication with each such section for controlling the pressure between the respective reactor sections.30. The process of claim 6, wherein the polycondensation reactor includes a top section, a middle section, and a bottom section, and wherein the pressure is reduced in the polycondensation reactor, the reducing step comprising at least three degassing mechanisms incorporated into the polycondensation reactor so that the polycondensation fluids traversing within its inside surface also flow sequentially by the three respective degassing mechanisms when flowing from the first end to the second end of the polycondensation reactor, and wherein the three degassing mechanisms are located respectively at the top section, the middle section, and the bottom section of the polycondensation reactor.31. The process of claim 30, wherein the top, the middle, and the bottom sections of the polycondensation reactor are maintained at different pressures from each other.32. The process of claim 7, wherein the esterification pipe reactor and the polycondensation pipe reactor both comprise substantially empty pipe.33. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing a combined esterification and prepolymer polycondensation pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester oligomer within the pipe reactor and the polyester oligomer exits from the outlet thereof, wherein the reactants and the polyester oligomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a polycondensation pipe reactor formed separately of the combined esterification prepolymer pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification/prepolymer pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester oligomer into the first end of the polycondensation pipe reactor so that the oligomer flows through the polycondensation reactor, the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the oligomer and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 34. A process for making a polyester polymer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a polycondensation pipe reactor integrally combined with the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 35. A process for making a polyester oligomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a prepolymer polycondensation pipe reactor formed separately of the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form the oligomer within the polycondensation pipe reactor, and the oligomer exits from the second end of the reactor, wherein the monomer and the oligomer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 36. A process for making a polyester oligomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor and react with each other to form a polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; (c) providing a prepolymer polycondensation pipe reactor integrally combined with the esterification pipe reactor, the polycondensation pipe reactor in fluid communication with the esterification pipe reactor, the polycondensation pipe reactor having a first end, a second end, and an inside surface; and (d) directing the fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form the oligomer within the polycondensation pipe reactor, and the oligomer exits from the second end of the reactor, wherein the monomer and the oligomer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 37. The process of claim 8, wherein the at least one weir is dispersed proximal to the outlet of the esterification pipe reactor.38. The process of claim 37, wherein the weir has a body portion circumscribed by an edge, a portion of the edge being a connecting edge and a remaining portion of the edge being a top edge, the connecting edge being of a size to be complementarily received by a portion of the inside surface of the esterification reactor and attached thereto, wherein the weir acts as a barrier for the esterification fluids so that the esterification fluids flow over the top edge of the weir when flowing from the inlet to the outlet of the esterification reactor.39. The process of claim 38, wherein the body portion of the weir has at least two opposed sides, the weir further defining at least one opening in one of said sides and extending therethrough such that the esterification fluids flow through the at least one opening as well as over the top edge of the weir when flowing through the weir.40. The process of claim 8, wherein a section of the body portion of the weir is detachably removed in order to allow the esterification fluids to pass therethrough instead of over the top edge of the weir.41. The process of claim 37, wherein the interior surface of the esterification reactor has an inner diameter, the esterification reactor further comprising a reducer located immediately downstream of the weir, the reducer having a diameter less than the inner diameter of the esterification reactor upstream and downstream of the reducer.42. The process of claim 41, wherein the reducer has a lower end with an aperture defined therein and through which the esterification fluids flow when traversing from the upstream section of the reactor to the downstream section thereof, the lower end of the reducer being spaced from the inside surface of the downstream section.43. The process of claim 42, wherein the lower end of the reducer is spaced from a top surface of the esterification fluids flowing through the downstream section of the reactor.44. The process of claim 9, wherein the weir has a body portion circumscribed by an edge, a portion of the edge being a connecting edge and a remaining portion of the edge being a top edge, the connecting edge being of a size to be complementarily received by a portion of the inside surface of the polycondensation reactor and attached thereto, wherein the weir acts as a barrier for the polycondensation fluid so that the polycondensation fluids flow over the top edge of the weir when flowing from the first end to the second end of the polycondensation reactor.45. The process of claim 44, wherein the body portion of the weir has opposed sides, the opposed sides defining at least one opening therebetween, and wherein the polycondensation fluids flow through the opening as well as over the to edge of the weir.46. The process of claim 9, wherein a section of the body portion of the weir is detachably removable to allow the polycondensation fluids to pass therethrough instead of over the top edge of the weir.47. The process of claim 6 or 9, wherein the polycondensation reactor is formed as a plurality of contiguous interconnected sections in which the polycondensation fluids flow through the inside surface of each section traversing from the first and to the second end of the polycondensation reactor.48. The process of claim 47, wherein each section of the polycondensation reactor forms an angle with a vertically-oriented plane, the angle being greater than zero degrees.49. The process of claim 47, wherein the polycondensation reactor further comprises at least one weir attached to the inside surface thereof, the at least one weir being located adjacent a juncture of each of the interconnected reactor sections.50. The process of claim 49, wherein the weir has a body portion circumscribed by an edge, a portion of the edge being a connecting edge and a remaining portion of the edge being a top edge, the connecting edge being of a size to be complementarily received by a portion of the inside surface of the polycondensation reactor and attached thereto, wherein the weir acts as a barrier so that the polycondensation fluids flow over the top edge of the weir.51. The process of claim 50, wherein the body portion of the weir has opposed sides, the opposed sides defining at least one opening therebetween, wherein the polycondensation fluids flow through the opening as well as over the to edge of the weir.52. The process of claim 49, wherein the inside surface of the polycondensation reactor has an inner diameter, the polycondensation reactor further comprising a reducer located immediately downstream of each respective weir, the reducer having a diameter smaller than the inner diameter of the adjacent polycondensation reactor sections upstream and downstream of the reducer.53. The process of claim 52, wherein the reducer forms a part of the juncture of each pair of interconnected reactor sections formed by an upstream section and a downstream section, the reducer being connected to the upstream section and extending into the downstream section.54. The process of claim 53, wherein the reducer has a lower end having an aperture through which the polycondensation fluids flow when traversing from the upstream section to the downstream section of the reactor, the lower end of the reducer being spaced from the inside surface of the downstream section.55. The process of claim 54, wherein the lower end of the reducer is spaced from a top surface of the polycondensation fluids flowing through the downstream section.56. The process of claim 6, wherein the esterification fluids are not recirculated.57. The process of claim 11, wherein the effluent from the recirculation is directed to the esterification reactor proximate the inlet of the esterification reactor.58. The process of claim 11, wherein the effluent from the recirculation is directed to the esterification reactor adjacent the inlet of the esterification reactor.59. The process of claim 11, wherein the effluent from the recirculation is directed to the esterification reactor between the inlet and the outlet of the esterification reactor.60. The process of claim 11, wherein the effluent from the recirculation is directed to the esterification reactor upstream of the inlet of the esterification reactor.61. The process of claim 11, wherein the influent to the recirculation is in fluid communication with the esterification reactor between the inlet and outlet thereof.62. The process of claim 11, wherein the influent to the recirculation is in fluid communication with the esterification reactor proximate the outlet thereof.63. The process of claim 11, wherein the influent to the recirculation is in fluid communication with the polycondensation reactor.64. The process of claim 11, wherein the influent to the recirculation is in fluid communication with the polycondensation reactor proximate the outlet thereof.65. The process of claim 11, wherein the recirculating step is performed using a recirculation loop having an influent and an effluent, the effluent being fluid communication with the pipe reactor proximal the inlet, wherein the fluids flowing through the recirculation loop are each recirculation fluids.66. The process of claim 65, wherein the influent being in fluid communication with the pipe reactor between the inlet and outlet thereof or proximal the outlet thereof.67. The process of claim 65, wherein the recirculation loop further comprises a recirculation pump located intermediate the influent and the effluent thereof for increasing the pressure of the recirculation fluids flowing therethrough.68. The process of claim 67, further comprising decreasing the pressure of the recirculation fluids at a location downstream of the recirculation pump.69. The process of claim 68, wherein the pressure decreasing step is performed using a pressure decreasing device of an eductor, a siphon, an exhauster, a venturi nozzle, a jet or an injector through which at least a portion of the recirculation fluids flow.70. The process of claim 68, wherein the pressure decreasing step is performed using an eductor.71. The process of claim 69, further comprising feeding at least one type of solid reactant into the recirculation loop which is dissolved by the recirculation fluids before flowing to the effluent of the recirculation loop.72. The process of claim 71, wherein the feeding step is performed using a feeding conduit having a discharge end in fluid communication with the recirculation loop adjacent or at the pressure decreasing device, wherein the reactant is drawn into the recirculation loop from the decreased pressure of the recirculation fluid developed by the pressure decreasing device.73. The process of claim 72, wherein the pressure decreasing device comprises an eductor.74. The process of claim 72, wherein the recirculating step and the feeding step collectively perform the step of adding at least one type of a reactant into the pipe reactor proximal the inlet.75. The process of claim 72, including a feeding conduit having receiving end opposed to a discharge end, and wherein die feeding step further comprises:(a) a reactant storage device for storing the reactant to be fed into the recirculation loop; (b) a solid metering device for receiving the reactant from the solid reactant storage device; and (c) a loss in weight feeder in communication with the solid metering device and also in communication with the receiving end of the feeding conduit, wherein the reactant is fed into the recirculation loop from the solid reactant storage device, to the solid metering device, into the loss in weight feeder, and then through the feeding conduit to be drawn into the recirculation line adjacent the pressure decreasing device. 76. The process of claim 71, wherein the reactant fed into the recirculation loop is terephthalic acid.77. The process of claim 76, further comprising injecting a second reactant, which is a fluid, into the recirculation loop upstream of the pressure decreasing device.78. The process of claim 76, further comprising injecting a second reactant, which is a fluid, into the recirculation loop downstream of the pressure decreasing device.79. The process of claim 76, further comprising injecting a second reactant, which is a fluid, into the recirculation loop through a recirculation pump seal.80. The process of claim 77, wherein the recirculating step, the feeding step, and the injecting step collectively perform the step of adding at least two types of reactants into the pipe reactor proximal the inlet thereof.81. The process of claim 77, 78 or 79, wherein the second reactant is ethylene glycol.82. The process of claim 68, further comprising removing vapors from the recirculation loop proximal to its influent and upstream of the pump, between the pump and the pressure decreasing device, or downstream of the pressure decreasing device.83. The process of claim 82, wherein the removing step comprises a vent incorporated into the recirculation loop so that the recirculation fluids flow through the vent when flowing from the influent to the effluent of the recirculation loop.84. The process of claim 83, wherein the vent reduces the flow rate of the recirculation fluids to create a stratified flow regime.85. The process of claim 83, wherein the vent comprises a flat-on-bottom reducer.86. The process of claim 83, wherein the vent is substantially horizontally disposed so that the recirculation fluids flowing therethrough are flowing substantially horizontally.87. The process of claim 86, wherein the vent further comprises upstanding degas stand pipe coupled to the vent, wherein the degas stand pipe has receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the receiving end.88. The process of claim 87, wherein the degas stand pipe is non-linear extending in its lengthwise direction between its receiving end and its venting end, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the venting mechanism, a second section coupled to the first section and oriented at about a forty-five degree angle relative to the first section in plan view, and a third section coupled to the second section and oriented at about a forty-five degree angle relative to the second section in plan view so that the third section is oriented substantially horizontally.89. The process of claim 87, wherein the venting end of the degas stand pipe is in fluid communication with ambient so that the pressure of the venting the end is at substantially atmospheric pressure.90. The process of claim 87, wherein the degas stand pipe further comprises a flow control device within the degas stand pipe for controlling the flow of fluids therethrough.91. The process of claim 90, wherein the flow control device comprises an orifice.92. The process of claim 83, wherein the recirculation loop comprises a plurality of elbows, a first elbow disposed upstream of the venting mechanism and a second elbow disposed downstream of the venting mechanism.93. The process of claim 65, further comprising feeding at least one type of reactant from a paste tank into the recirculation loop.94. The process of claim 12 or 13, wherein the vent reduces the flow rate of the fluids flowing therethrough to create a stratified flow regime.95. The process of claim 12 or 13, wherein the vent comprises a flat-on-bottom reducer.96. The process of claim 12 or 13, wherein the vent is substantially horizontally disposed so that the fluids flowing therethrough are flowing substantially horizontally.97. The process of claim 12 or 13, wherein the vent further comprises an upstanding degas stand pipe coupled to the vent, wherein the degas stand pipe has a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the inlet end.98. The process of claim 97, wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at about a forty-five degree angle relative to the first section in plan view, and a third section coupled to the second section and oriented at about a forty-five degree angle relative to the second section in plan view so that the third section is oriented substantially horizontally.99. The process of claim 97, wherein the venting end of the degas stand pipe is in fluid communication with ambient so that the pressure of the venting end is at substantially atmospheric pressure.100. The process of claim 97, wherein the degas stand pipe further comprises a flow control device within the degas stand pipe for controlling the flow of fluids therethrough.101. The process of claim 100, wherein the flow control device comprises an orifice.102. The process of claim 97, wherein the pipe reactor further comprises a plurality of elbows, a first elbow disposed upstream of the vent and a second elbow disposed downstream of the vent.103. The process of claim 97, wherein the venting end of the degas stand pipe is in fluid communication with a vacuum source so that a sub-atmospheric pressure exists in the standpipe and at the inside surface of the polycondensation reactor.104. The process of claim 97, wherein the polycondensation reactor includes a top section, a middle section, and a bottom section, and wherein the reducing step comprises at least three degassing mechanisms incorporated into the polycondensation reactor so that the polycondensation fluids traversing within its inside surface also flow sequentially by the three respective degassing mechanisms when flowing from the first end to the second end of the reactor, and wherein the three degassing mechanisms the located respectively at the top section, the middle section, and the bottom section of the reactor.105. The process of claim 104, wherein the top, the middle, and the bottom sections of the reactor are maintained at different pressures from each other.106. The process of claim 105, wherein the pressure in the top section is in the range of from 40 to 120 millimeters mercury, the pressure in the middle section is in the range of from 2 to 25 millimeters mercury, and the pressure in the bottom section is in the range of from 0.1 to 5 millimeters mercury.107. The process of claim 104, wherein the three degassing mechanisms are in fluid communication with a single vacuum source and a single condenser system.108. The process of claim 97, wherein the degas stand pipe is non-linear extending in its lengthwise direction between its receiving end and its venting end.109. The process of claim 108, wherein the degas stand pipe is formed of at least two contiguous sections, each such section being in fluid communication with the other, and wherein the outlet of each such section is positioned horizontally with or disposed vertically above the inlet of each respective section.110. The process of claim 109, wherein the contiguous section adjacent the venting end is oriented substantially horizontally.111. The process of claim 6, further comprising heating the fluids flowing through the pipe reactor.112. The process of claim 111, wherein the pipe reactor has an exterior surface, and wherein the heating step comprises placing a heat transfer media in thermal communication with a portion of the exterior surface of the pipe reactor along at least a lengthwise portion of the pipe reactor between the inlet or first end and the outlet or second end thereof of the esterification and/or the polycondensation reactor, respectively.113. The process of claim 112, wherein the beat transfer media comprise a plurality of electrical heating components wrapped about the exterior surface of the pipe reactor.114. The process of claim 111, wherein the pipe reactor has an exterior surface, and wherein the heating step comprises:(a) a jacket pipe circumscribing the exterior surface of the pipe reactor along a portion of the length thereof between the inlet and outlet, the jacket pipe having an inner surface larger than the exterior surface of the pipe reactor for forming an annular space therebetween; and (b) supplying heat transfer media within the annular space formed between the exterior surface of the pipe reactor and the inner surface of the jacket pipe. 115. The process of claim 114, wherein the heat transfer media comprises a liquid, a vapor, a steam, electrical heating components, or a combination thereof.116. The process of claim 115, wherein the heat transfer media comprises a combination of liquid and steam that flows within the annular space in a direction counter to the direction of the reactant flowing through the pipe reactor.117. The process of claim 113, wherein the heating step comprise passing the reactants and the monomers through a heat exchanger located in the pipe reactor within a recirculation loop positioned at an intermediate point between the respective ends of the esterification reactor.118. The process of claim 111, wherein the heating step comprise passing the reactants and the monomers through a heat exchanger disposed proximate and in fluid communication with the outlet of the esterification pipe reactor.119. The process of claim 118, wherein the heat exchanger is in fluid communication with and is proximate to or within a seal leg.120. The process of claim 111, wherein the heating step comprise passing the polycondensation fluids through a heat exchanger positioned intermediate the first end and the second end of the polycondensation pipe reactor.121. The process of claim 6, wherein at least one of the reactants is added in a heated state or as a hot vapor.122. The process of claim 116, wherein the heat transfer media is moved through the annular space in the absence of a subloop pump.123. The process of claim 6, further comprising introducing an additive into the esterification or polycondensation pipe reactor.124. The process of claim 123, wherein the additive comprises a catalyst, a coreactant, or a mixture thereof.125. The process of claim 123, wherein the additive comprises DEG, CHDM, or a combination of both.126. The process of claim 123, wherein the pipe reactor has an exterior surface and further comprises:(a) a sealable channel extending through the pipe reactor allowing fluid communication between its exterior surface and the interior surface of the pipe reactor; and (b) an injector for injecting the additive into the reactant flowing within the pipe reactor. 127. The process of claim 126, wherein the injector comprises a pump.128. The process of claim 126, wherein the pipe reactor further comprises at least one elbow, seal leg, or heat exchanger, and wherein the sealable channel traverses through a portion of the elbow or seal leg, or proximate to and upstream of the heat exchanger.129. The process of claim 123, wherein the additive is added by a gravity flow thereof passing into the pipe reactor.130. The process of claim 6, wherein the pressure of the reactant fluids at the interior surface of the pipe reactor adjacent the inlet is greater than the pressure of the reactant fluids at the interior surface of the reactor adjacent the outlet.131. The process of claim 130, wherein the adding step is preformed by a pump that discharges the reactants at a pressure substantially the same as the pressure at the interior surface of the reactor, adjacent the inlet thereof.132. The process of claim 130, wherein the pressure of the fluids flowing through the pipe reactor continually decreases as the fluids move from the inlet toward the outlet thereof.133. The process of claim 6, wherein the fluids flowing through the pipe reactor pass through a plurality of adjacent stages of increasing and decreasing fluid pressure zones, respectively, as the fluids move from the inlet toward the outlet of the reactor.134. The process of claim 6, wherein the esterification pipe reactor is substantially linear extending in its lengthwise direction between the inlet and the outlet thereof.135. The process of claim 6, wherein the esterification or polycondensation pipe reactor is non-linear extending in its lengthwise direction between the inlet and the outlet thereof.136. The process of claim 135, wherein the pipe reactor is serpentine in front plan view.137. The process of claim 135, wherein the pipe reactor further comprises a plurality of elbows, each elbow changing the direction of the fluid flow within the pipe reactor relative to a stationary horizontal plane.138. The process of claim 135, wherein the pipe reactor is constructed is arranged to obtain a predetermined pressure profile, in which the pressure of the reactant is substantially constant along a portion of the pipe reactor extending horizontally, and the pressure of the reactant decreases at an increasing rate along a portion of the inner surface of the pipe reactor as that portion of the pipe reactor extends in a more vertical orientation.139. The process of claim 6, wherein a first stage of the polycondensation pipe reactor having an inlet and an outlet, is positioned wherein the inlet to the polycondensation pipe reactor is adjacent, vertically above, and in fluid communication with the outlet of the esterification pipe reactor.140. The process of claim 6, wherein gravity moves the polycondensation fluids from the first end toward the second end of the reactor.141. The process of claim 6, wherein the polycondensation reactor is divided into a plurality of substantially parallel flow conduits extending between the end and the second end thereof, and wherein fluid flowing through the polycondensation reactor passes through one of the plurality of flow conduits while flowing therethrough.142. The process of claim 6, wherein the polycondensation reactor is substantially linear extending in its lengthwise direction between its first end and its second end.143. The process of claim 6, wherein the polycondensation piper reactor is disposed in a substantially vertical orientation.144. The process of claim 28, wherein the seal leg has a heat exchanger disposed proximate to the seal leg or within the seal leg for heating the esterification fluid.145. The process of claim 29, wherein at least one seal leg has a heat exchanger disposed proximate to the seal leg or within the seal leg for heating the polycondensation fluid.146. The process of claim 6, wherein the polycondensation reactor has at least two sections of a first section and a second section, and wherein the pressure is reduced in the polycondensation reactor, the reducing step comprising at least two degassing mechanisms incorporated into the polycondensation reactor so that the polycondensation fluids traversing within its inside surface also flow sequentially by the two respective degassing mechanisms when flowing from the first end to the second end of the polycondensation reactor, and wherein the two degassing mechanisms the located respectively at the first section and the second section of the polycondensation reactor.147. The process of claim 6, wherein the first and second section of the polycondensation reactor are maintained at different pressures from each other.148. The process of claim 6, wherein the reactants comprise terepthalic acid and ethylene glycol.149. The process of claim 6, wherein the reactants comprise dimethyl terephthalate and ethylene glycol.150. The process of claim 6, wherein the reactants comprise terepthalate acid, ethylene glycol and CHDM.151. The process of claim 6, wherein the polyester is PET, PETG poly(cyclohexane)-dimethylene terephthalate, polyester formed from CHDM and dimethyl cyclohexanedicarboxylate, a liquid crystalline polyester, or a biodegradable polyester.152. The process of claim 6, wherein the polyester is PET.153. The process of claim 6, wherein the polyester is PETG.154. The process of claim 6, wherein the polyester is not polycarbonate or PBT, or a reactant of phthalic anhydride or maleic anhydride.155. The process of claim 6, wherein at least two reactants are added into the pipe reactor proximal the inlet thereof.156. The process of claim 148, wherein in the adding step, the terephthalic acid is pumped from a paste mix tank into the pipe reactor proximal the inlet thereof.157. The process of claim 6, wherein the pipe reactor divides into a plurality of substantially parallel flow conduits extending between the inlet and the outlet thereof, and wherein the reactant flowing through the pipe reactor passes through one of the plurality of flow conduits while flowing through the reactor.158. The process of claim 6, wherein at least two separate esterification pipe reactors are provided, each of which produces the same or a different polyester monomer, and wherein the fluid polyester monomer exiting the respective esterification pipe reactors is directed into the first end of the polycondensation pipe reactor.159. The process of claim 158, wherein at least two separate polycondensation pipe reactors are provided, each of which produces the same or a different polyester polymer, and wherein each fluid polyester monomer exiting the respective esterification pipe reactors is directed to the first end of at least one of the respective polycondensation pipe reactors.160. The process of claim 6, wherein at least two separate polycondensation pipe reactors are provided, each of which produces the same or a different polyester polymer, and wherein the fluid polyester monomer exiting the esterification pipe reactor is directed into the respective first ends of each of the polycondensation pipe reactors.161. The process of claim 6, wherein the esterification pipe reactor comprises a plurality of esterification reactors positioned in parallel to one another with a common inlet.162. The process of claim 6, wherein the polycondensation piper reactor comprises a plurality of polycondensation reactors positioned in parallel to one another with a common first end.163. The process of claim 162, wherein a co-reactant is added to at least one of the plurality of polycondensation reactors but not to all of the polycondensation reactors to thereby produce at least two different polyester products.164. The process of claim 6, wherein the interior surface and inside surface is substantially circular in cross section.165. The process of claim 6, wherein the esterification or polycondensation pipe reactor interior surface is formed of a catalytic material.166. The process of claim 6, wherein at least one reactant is a diol compound, and wherein at least a portion of the diol compound is removed from the process as a vapor, a liquid, or as both a vapor and a liquid, and is subjected to an adsorption system to selectively recover the diol compound.167. A process for making a polyester monomer from plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, an interior surface, and at least one weir attached to the interior surface thereof; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid, and wherein the esterification fluids flow over the weir. 168. A process for making a polyester monomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, and wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; and (c) recirculating a portion of the process fluids and directing the recirculation effluent back to and therethrough the esterification reactor proximate the inlet of the esterification reactor or between the inlet and outlet of the esterification reactor. 169. A process for making a polyester monomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid; and (c) removing vapors from the pipe reactor intermediate its inlet and its outlet and/or proximate its outlet through a vent of empty pipe. 170. A process for making a polyester monomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface, the inlet being positioned at least 20 vertical feet below the outlet; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, and wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid. 171. A process for making a polyester monomer from a plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid, and wherein the fluids present in the pipe reactor are in a bubble or froth flow regime. 172. A process for making a polyester monomer from plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface, wherein the pipe reactor has alternating linear and monomer sections extending in its lengthwise direction between the inlet and outlet thereof; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the reactants and the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid. 173. A process for making a polyester monomer from plurality of reactants, comprising:(a) providing an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) adding at least one reactant into the pipe reactor proximal the inlet so that the reactants flow through the pipe reactor, the reactants reacting with each other to form the polyester monomer within the pipe reactor and the polyester monomer exits from the outlet thereof, wherein the at least one reactant the polyester monomer flowing through the esterification pipe reactor are each an esterification fluid. 174. The process of one of claims 167-173, wherein the pipe reactor comprises substantially empty pipe.175. The process of claim 173, further comprising a seal leg positioned between and in fluid communication with the esterification process and a polycondensation process for controlling the pressure between the esterification and polycondensation processes.176. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, and an inside surface, the first end being disposed vertically above the second end, the polycondensation pipe reactor having alternating linear and non-linear sections extending in its lengthwise direction between its first the end and its second end; wherein the polycondensation pipe reactor is operated in a least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 177. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, an inside surface, and at least one weir attached to the inside surface thereof, wherein the pipe reactor is made of a substantially empty pipe; wherein the polycondensation pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid, and wherein at least one of the polycondensation fluids flows over the weir. 178. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, and an inside surface; wherein the polycondensation pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid; and (c) removing vapors from the pipe reactor intermediate its inlet an its outlet and/or proximate its inlet or outlet through a vent comprising substantially empty pipe. 179. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, and an inside surface; wherein the polycondensation reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacting to form an oligomer and then the oligomer reacting to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid, and wherein the fluids present in the pipe the reactor are in a stratified flow regime. 180. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, and an inside surface; wherein the polycondensation pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester monomer into the first end of the polycondensation pipe reactor so that the monomer flows through the polycondensation reactor, the monomer reacts to form an oligomer and then the oligomer reacts to form the polymer within the polycondensation pipe reactor, and the polymer exits from the second end of the reactor, wherein the monomer, the oligomer, and the polymer flowing through the polycondensation pipe reactor are each a polycondensation fluid. 181. The process of one of claims 176, 178, 179, or 180, wherein the pipe reactor comprises a substantially empty pipe.182. The process of one of claims 176, 177, or 178, wherein the fluids present within the pipe reactor are in a stratified flow regime.183. The process of one of claims 177-179, wherein the polycondensation pipe reactor has alternating linear and non-linear sections extending in its lengthwise direction between its first end and its second end.184. The process of claim 180, wherein the polycondensation pipe reactor is substantially horizontally oriented.185. The process of claim 180, wherein the polycondensation reactor includes at least two different sections in fluid communication with one another, each section being of a different fluid pressure, and wherein a seal leg is positioned between and in fluid communication with each such section for controlling the pressure between the respective reactor sections.186. The process of claim 180, wherein the polycondensation reactor includes a top section, a middle section, and a bottom section, and wherein the vapor is reduced in the polycondensation reactor, the reducing step comprising at least three degassing mechanisms incorporated into the polycondensation reactor so that the polycondensation fluids traversing within its inside surface also flow sequentially by the three respective degassing mechanisms when flowing from the first end to the second end of the polycondensation reactor, and wherein the three degassing mechanisms are located respectively at the top section, the middle section, and the bottom section of the polycondensation reactor.187. The process of claim 186, wherein the top, the middle, and the bottom sections of the polycondensation reactor are maintained at different pressures from each other.188. A process for making a polyester polymer, comprising:(a) providing a polycondensation pipe reactor having a first end, a second end, and an inside surface; wherein the polycondensation pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) directing a fluid polyester oligomer into the first end of the polycondensation pipe reactor so that the oligomer flows through the polycondensation pipe reactor, the oligomer reacting to form the polyester polymer within the polycondensation pipe reactor and the polyester polymer exits from the second end thereof. 189. An apparatus for producing a polyester oligomer polymer, comprising:(a) an esterification pipe reactor having an inlet, an outlet, and an interior surface through which esterification fluid reactants are passed; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) a polycondensation pipe reactor formed separately of and in fluid communication with the esterification reactor, wherein the polycondensation reactor has an inlet, an outlet, and an interior surface through which at least one polycondensation fluid reactant is passed, wherein the esterification and polycondensation reactors comprise substantially empty pipe. 190. An apparatus for producing a polyester oligomer polymer, comprising:(a) an esterification pipe reactor having an inlet, an outlet, and an interior surface through which esterification fluid reactants are passed; wherein the esterification pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) a polycondensation pipe reactor formed separately of and in fluid communication with the esterification reactor, wherein the polycondensation reactor has an inlet, an outlet, and an interior surface through which at least one polycondensation fluid reactant is passed. 191. The apparatus of claim 190, further comprising a recirculation loop having an influent and an effluent, the effluent being in fluid communication with the esterification pipe reactor.192. The apparatus of claim 190, further comprising at least one weir attached to the interior surface of the esterification pipe reactor and wherein the esterification fluids flow over the weir.193. The apparatus of claim 190, further comprising at least one weir attached to the interior surface of the polycondensation pipe reactor and wherein the polycondensation fluids flow over the weir.194. The apparatus of claim 190, further comprising a vent in fluid communication with the esterification reactor, the vent further comprising an upstanding degas stand pipe coupled to the vent, the degas stand pipe having a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the receiving end, and wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at an angle relative to the first section in plan view, and a third section coupled to the second section and oriented at a complimentary angle relative to the second section in plan view so that the third section is oriented substantially horizontally.195. The apparatus of claim 190, further comprising a vent in fluid communication with the polycondensation reactor, the vent further comprising an upstanding degas stand pipe coupled to the vent, the degas stand pipe having a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the receiving end, and wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at an angle relative to the first section in plan view, and a third section coupled to the second section and oriented at a complimentary angle relative to the second section in plan view so that the third section is oriented substantially horizontally.196. The apparatus of claim 190, wherein the esterification piper reactor inlet is positioned at least 20 vertical feet below the esterification pipe reactor outlet.197. The apparatus of claim 190, wherein the polycondensation pipe reactor is substantially horizontally oriented.198. The apparatus of claim 190, wherein the esterification piper reactor and polycondensation pipe reactor each have alternating linear and non-linear sections extending in their respective lengthwise direction between the respective inlets and outlets thereof.199. The apparatus of claim 190, further comprising a seal leg positioned between and in fluid communication with the esterification reactor and the polycondensation reactor for controlling the pressure between the esterification and polycondensation reactors.200. The apparatus of claim 190, wherein the polycondensation reactor includes at least two different sections in fluid communication with one another, each section being of a different fluid pressure, and wherein a seal leg is positioned between and in fluid communication with each such section for controlling the pressure between the respective reactor sections.201. The apparatus of claim 190, wherein the polycondensation reactor includes a top section, a middle section, and a bottom section, and further comprising at least three degassing mechanisms incorporated into the polycondensation reactor that the polycondensation fluids traversing within its inside surface also flow sequentially by the three respective degassing mechanisms when flowing from the first end of the second end of the polycondensation reactor, and wherein the three degassing mechanisms are located and are in fluid communication with respectively the top section, the middle section, and the bottom section of the polycondensation reactor.202. The apparatus of one of claims 191-201, wherein the esterification pipe reactor and the polycondensation pipe reactor both comprise substantially empty pipe.203. An esterification pipe reactor apparatus for producing a polyester monomer, comprising:(a) an esterification pipe reactor having an inlet, an outlet, and an interior surface; wherein the esterification pipe reactor is operated in at least on flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) a recirculation loop having an influent and an effluent, the effluent being in fluid communication with the esterification pipe reactor. 204. The apparatus of one of claim 191 or 203, wherein the effluent is in fluid communication with the reactor adjacent the inlet thereof.205. The apparatus of one of claim 191 or 203, wherein the effluent is in fluid communication with the reactor between the inlet and outlet thereof.206. The apparatus of one of claim 191 or 203, wherein the influent is in fluid communication with the reactor between the inlet and outlet thereof.207. The apparatus of one of claim 191 or 203, wherein the influent is in fluid communication with the reactor proximate the outlet thereof.208. The apparatus of one of claim 191 or 203, wherein the influent is in fluid communication with a second reactor, wherein the second reactor is do stream of the esterification reactor.209. An apparatus for producing a polyester monomer, oligomer, or polymer, comprising:(a) a pipe reactor having an inlet, an outlet, and an interior surface through which the fluid reactants are passed; and (b) a weir connected to a portion of the interior surface of the piper reactor and adjacent the outlet thereof, wherein the pipe reactor is operated at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and wherein the reactor comprises substantially empty pipe. 210. An apparatus for producing a polyester monomer, oligomer, or polymer, comprising:(a) a pipe reactor having an inlet, an outlet, and an interior surface through which the fluid reactants are passed; wherein the pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow; and (b) a vent in fluid communication with the reactor, the vent further comprising an upstanding degas stand pipe coupled to the vent, the degas stand pipe having a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the receiving end, and wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at an angle relative to the first section in plan view, and a third section coupled to the second section and oriented at a complimentary angle relative to the second section in plan view so that the third section is oriented substantially horizontally. 211. The apparatus of claim 210, wherein the vent is substantially horizontally disposed so that the fluids flowing therethrough are flowing substantially horizontally.212. The apparatus of claim 210, wherein the first section is oriented at from about a 10 to about an 80 degree angle relative to the first section, and the section is oriented at from about an 80 to about a 10 degree angle relative to the second section.213. The apparatus of claim 210, wherein the first section is oriented at about a 45 degree angle relative to the first section and the third section is oriented about a 45 degree angle relative to the second section.214. An apparatus for producing a polyester monomer, oligomer, or polymer comprising:(a) a pipe reactor having an inlet, an outlet, and an interior surface through which the fluid reactants are passed; wherein the pipe reactor has alternating linear and non-linear sections extending in their respective lengthwise directions between the inlet and outlet thereof; and wherein the pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow. 215. The apparatus of one of claim 203 or 210, wherein the reactor comprises substantially empty pipe.216. The apparatus of claim 214, wherein the pipe reactor inlet is positioned at least 20 vertical feet below the pipe reactor outlet.217. The apparatus of claim of 214, wherein the pipe reactor is substantially horizontally oriented.218. The apparatus of claim 214, wherein the reactor comprises substantially empty pipe.219. The apparatus of claim 214, further comprising a seal leg in fluid communication with and proximate the outlet of the reactor.220. The apparatus of claim 214, wherein the reactor includes at least two different sections in fluid communication with one another, each section being of different fluid pressure, and wherein a seal leg is positioned between and in fluid communication with each such section for controlling the pressure between the respective reactor sections.221. The apparatus of claim 214, wherein the reactor includes a top section, a middle section, and a bottom section, and further comprising at least three degassing mechanisms incorporated into the reactor so that the fluids traversing within its inside surface also flow sequentially by the three respective degassing mechanism when flowing from the first end to the second end of the reactor, and wherein the three degassing mechanisms are located and are in fluid communication with respectively the top section, the middle section, and the bottom section of the reactor.222. The apparatus of claim 190, further comprising a convention reactor for making a polyester monomer or polymer, wherein the esterification or polycondensation pipe reactor apparatus is constructed and arranged to be placed in fluid communication with the conventional reactor.223. The apparatus of claim 222, wherein the conventional reactor is a CSTR or reactive distillation, stripper, or rectification column.224. The apparatus of claim 222, wherein the pipe reactor is connected in series with the conventional reactor.225. The apparatus of claim 222, wherein the pipe reactor is connected in parallel to the conventional reactor.226. The apparatus of claim 190, further comprising:(a) a plurality of vent lines, each said vent line having a first end a spaced second end, and a vent header having a first end and a spaced second end, the first end of each respective vent line being connected to the vent discharge of each process, and the second end of each respective vent line being connected to the first end of the vent header; and (b) the second end of the vent header being connected to an oxidizer. 227. The apparatus of claim 226, wherein the oxidizer is an HTM furnace, an incinerator, or a thermal oxidizer.228. The apparatus of claim 226, wherein the vent header is under vacuum.229. The apparatus of claim 190, further comprising a continuous roof over each polyester polymer process building, truck unloading and pump station, and oxidizer, thereby eliminating the need for a wastewater treatment facility.230. The apparatus of claim 190, further comprising a column constructed and arranged to condense the vapor from the process, the column having a base, the volume of the base being sufficiently large enough to eliminate the need for column feed and product tanks.231. The apparatus of claim 230, wherein the column is a water column, MGM column, or stripper column.232. A polyester production system, comprising the pipe reactor apparatus of claim 190, retrofitted to a conventional polyester process comprising a conventional polyester reactor, wherein the conventional reactor has been disabled from the production system.233. A method of retrofitting a pipe reactor to a conventional polyester process comprising:(a) retrofitting the pipe reactor apparatus of claim 190 in a conventional polyester process comprising a conventional polyester reactor; and (b) disabling the conventional reactor from the process. 234. An apparatus for venting a process of gas or vapor while effectively disengaging liquid from the gas or vapor, the liquid, gas and vapor being fluids, separating the liquid from the gas or vapor, and returning the liquid back to the process, comprising:(a) a vessel or process pipe containing (i) liquid and (ii) gas or vapor; and (b) a vent in fluid communication with the vessel or process pipe, the vent further comprising an upstanding degas stand pipe coupled to the vent, the degas stand pipe having a receiving end in fluid communication with the vent and an opposed venting end disposed vertically above the receiving end, and wherein the degas stand pipe is non-linear extending in its lengthwise direction between the receiving end and the venting end thereof, and wherein the degas stand pipe is formed of three contiguous sections each in fluid communication with each other, a first section adjacent the receiving end and extending substantially vertically from the vent, a second section coupled to the first section and oriented at an angle relative to the first section in plan view, and a third section coupled to the second section and oriented at an angle relative to the second section in plan view so that the third section is oriented substantially horizontally; wherein the pipe reactor is operated in at least one flow regime selected from the group consisting of bubble flow, plug flow, stratified flow, wavy flow, slug flow, dispersed flow and froth flow. 235. The apparatus of claim 234, wherein at least apart of the vent upstream of the first section is substantially horizontally disposed so that the fluids flowing therethrough are flowing substantially horizontally.236. The apparatus of claim 234, wherein the first section is oriented at from about a 0 to about a 60 degree angle relative to the vertical plane, the second section is oriented at from about aa 5 to about an 85 degree angle relative to the vertical plane, and the third section is oriented at from about a 0 to about a 45 degree angle relative to the horizontal plane.237. The apparatus of claim 234, wherein the first section is oriented at about a 0 degree angle relative to the vertical plane, the second section is oriented at about a 45 degree angle relative to the vertical plane, and the third section is oriented at about a 0 degree angle relative to the horizontal plane.238. The process of claim 184, wherein the polycondensation pipe reactor has a length of at least 20 feet.239. The process of claim 184, wherein the polycondensation pipe reactor has a length of at least 60 feet.240. The process of claim 238 or 239, wherein the first end is disposed vertically above the second end, and the polycondensation fluids flow down the pipe the reactor by gravity.241. The process of claim 240, wherein the pipe reactor comprise substantially empty pipe.242. The apparatus of claim 214, wherein the pipe reactor has a length of at least 20 feet.243. The apparatus of claim 214, wherein the pipe reactor has a length of at least 60 feet.