CA2527042A1 - Polyester process using a pipe reactor - Google Patents

Polyester process using a pipe reactor Download PDF

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Publication number
CA2527042A1
CA2527042A1 CA002527042A CA2527042A CA2527042A1 CA 2527042 A1 CA2527042 A1 CA 2527042A1 CA 002527042 A CA002527042 A CA 002527042A CA 2527042 A CA2527042 A CA 2527042A CA 2527042 A1 CA2527042 A1 CA 2527042A1
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Prior art keywords
pipe reactor
flow
heat transfer
fluid
transfer media
Prior art date
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CA002527042A
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French (fr)
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CA2527042C (en
Inventor
Bruce Roger Debruin
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Eastman Chemical Co
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Eastman Chemical Company
Bruce Roger Debruin
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Application filed by Eastman Chemical Company, Bruce Roger Debruin filed Critical Eastman Chemical Company
Publication of CA2527042A1 publication Critical patent/CA2527042A1/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0042—Degasification of liquids modifying the liquid flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/432—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction with means for dividing the material flow into separate sub-flows and for repositioning and recombining these sub-flows; Cross-mixing, e.g. conducting the outer layer of the material nearer to the axis of the tube or vice-versa
    • B01F25/4323—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction with means for dividing the material flow into separate sub-flows and for repositioning and recombining these sub-flows; Cross-mixing, e.g. conducting the outer layer of the material nearer to the axis of the tube or vice-versa using elements provided with a plurality of channels or using a plurality of tubes which can either be placed between common spaces or collectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • B01F25/53—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle in which the mixture is discharged from and reintroduced into a receptacle through a recirculation tube, into which an additional component is introduced
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • C—CHEMISTRY; METALLURGY
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    • C08F2/00—Processes of polymerisation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
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    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
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    • C08G63/78—Preparation processes
    • C08G63/785—Preparation processes characterised by the apparatus used
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/08—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/08—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag
    • F28D7/082—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag with serpentine or zig-zag configuration
    • F28D7/085—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag with serpentine or zig-zag configuration in the form of parallel conduits coupled by bent portions
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

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.

Claims (101)

1. A method of producing a composition of matter, said method comprising:
(a) generating a gaseous fluid from a liquid fluid;
(b) forming a stratified flow regime in a pipe reactor with the liquid fluid and the gaseous fluid; and (c) separating at least a portion of the gaseous fluid from the liquid fluid proximate a location where the liquid and gaseous fluids are in stratified flow.
2. The method according to claim 1 wherein said gaseous fluid generated in step (a) is substantially the only gas-phase fluid present in the stratified flow regime.
3. The method according to claim 1 wherein said stratified flow regime is formed in a substantially horizontal section of the pipe reactor.
4. The method according to claim 1 wherein step (a) includes reacting at least a portion of the liquid fluid in the pipe reactor to thereby produce the gaseous fluid.
5. The method according to claim 4 wherein said reacting includes esterifying.
6. The method according to claim 4 wherein said reacting includes polycondensing.
7. The method according to claim 4 wherein said reacting includes forming the composition of matter in the liquid fluid.
8. The method according to claim 7 wherein said composition of matter has a terephthalate moiety.
9. The method according to claim 7 wherein said composition of matter is a condensation polymer.
10. The method according to claim 7 wherein said composition of matter is a polyester.
11. The method according to claim 7 wherein said composition of matter is PET.
12. The method according to claim 1 wherein step (a) includes heating the liquid fluid to thereby vaporize a portion thereof.
13. The method according to claim 1 wherein step (c) includes venting said at least a portion of the gaseous fluid from the pipe reactor.
14. The method according to claim 1 wherein step (c) includes reducing the flow velocity of the liquid and gaseous fluids to thereby cause disengagement of the liquid and gaseous fluids.
15. The method according to claim 1, further comprising:
(d) transporting the gaseous and liquid fluids upwardly in the pipe reactor by creating a pressure differential in the pipe reactor.
16. The method according to claim 1 wherein said pipe reactor has a generally serpentine configuration.
17. A method of producing a condensation polymer, said method comprising:
(a) condensing liquid monomers and/or liquid oligomers in a pipe reactor to thereby produce a gaseous condensation by-product and a liquid condensation mixture comprising the condensation polymer; and (b) causing the liquid condensation mixture and the gaseous condensation by-product to flow through at least a portion of the pipe reactor in a flow regime selected from the group consisting of stratified flow, wavy flow, slug flow, plug flow, bubble flow, froth flow, and combinations thereof.
18. The method according to claim 17 wherein said flow regime is stratified flow.
19. The method according to claim 17, further comprising the step of:
(c) disengaging at least a portion of the gaseous condensation by-product from the liquid
20. The method according to claim 19 wherein step (c) includes reducing the flow velocity of the gaseous condensation by-product and the liquid condensation mixture.
21. The method according to claim 19, further comprising the step of:
(d) removing the disengaged gaseous condensation by-product from the pipe reactor.
22. The method according to claim 17 wherein said condensation polymer is a polyester.
23. The method according to claim 17 wherein said condensation polymer is PET.
24. The method according to claim 17, further comprising the step of:
(e) forming the liquid monomers and/or the liquid oligomers in another pipe reactor.
25. The method according to claim 24 wherein said forming includes esterifying.
26. A method of producing a composition of matter, said method comprising:
(a) esterifying a liquid reactant in a pipe reactor to thereby produce a gaseous reaction by-product and a liquid reaction mixture comprising an ester reaction product of said esterifying; and (b) causing the liquid reaction mixture and the gaseous reaction by-product to flow through at least a portion of the pipe reactor in a flow regime selected from the group consisting of stratified flow, wavy flow, slug flow, plug flow, bubble flow, froth flow, and combinations thereof.
27. The method according to claim 26 wherein said flow regime is selected from the group consisting of bubble flow, froth flow, stratified flow, and combinations thereof.
28. The method according to claim 26 wherein said flow regime is stratified flow.
29. The method according to claim 26, further comprising:
(c) disengaging at least a portion of the gaseous reaction by-product from the liquid reaction mixture.
30. The method according to claim 29 wherein step (c) includes reducing the flow velocity of the gaseous reaction by-product and the liquid reaction mixture.
31. The method according to claim 29, further comprising:
(d) removing the disengaged gaseous reaction by-product from the pipe reactor.
32. The method according to claim 26 wherein said ester reaction product comprises a terephthalate moiety.
33. The method according to claim 26, further comprising:
(e) polycondensing the ester reaction product in another pipe reactor to thereby form a condensation polymer.
34. The method according to claim 33 wherein said condensation polymer is PET.
35. A process for making an ester from a plurality of reactants comprising:
(a) providing an esterification pipe reactor having a first inlet and a first outlet;
(b) adding the reactants under esterification reaction conditions into the esterification pipe reactor proximate to the first inlet and forming a two phase flow so the reactants form a liquid phase and vapor phase through the esterification pipe reactor, 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 wherein at least a portion of the reactants form an ester monomer.
36. The process of claim 35 wherein at least a portion of the ester monomer is reacted in the esterification pipe reactor to form an ester oligomer.
37. The process of claim 36 further comprising:
(c) reacting the ester oligomer under polycondensation reaction conditions in a polycondensation pipe reactor wherein at least a portion of the oligomer forms a polyester.
38. The process of claim 35 further comprising:
(c) reacting the ester monomer under polycondensation reaction conditions in a polycondensation pipe reactor wherein at least a portion of the ester monomer forms an ester oligomer.
39. The process of claim 38 further comprising:
(d) reacting the ester oligomer under polycondensation reaction conditions in the polycondensation pipe reactor wherein at least a portion of the oligomer forms a polyester.
40. The process of claim 35 wherein said reactants comprise a diacid or diacid generator and a diol or diol generator.
41. The process of claim 40 wherein said diacid or diacid generator is selected from the group consisting of aromatic dicarboxylic acids having 8 to 14 carbon atoms, aliphatic dicarboxylic acids having 4 to 12 carbon atoms, and cycloaliphatic dicarboxylic acids having 8 to 12 carbon atoms and esters of these diacids; and wherein said diol or diol generator is selected from the group consisting cycloaliphatic diols having 6 to 20 carbon atoms and aliphatic diols having 3 to 20 carbon atoms.
42. The process of claim 40 wherein said diacid or diacid generator and said diol or diol generator are selected from the group consisting of terephthalic acid, phthalic acid, isophthalic acid, naphthalene-2,6-dicarboxylic acid, cyclohexanedicarboxylic acid, cyclohexanediacetic acid, diphenyl-4,4'-dicarboxylic acid, dipheny-3,4'-dicarboxylic acid, 2,2,-dimethyl-1,3-propandiol, dicarboxylic acid, succinic acid, glutaric acid, adipic acid, azelaic acid, sebacic acid, dimethyl terephthalate, ethylene glycol, diethylene glycol, triethylene glycol, 1,4 -cyclohexane-dimethanol, propane-1,3-diol, pentane-1,5-diol, hexane-1,6-diol, neopentylglycol, 3-methylpentanediol-(2,4), 2-methylpentanediol-(1,4), 2,2,4-trimethylpentane-diol-(1,3), 2-ethylhexanediol-(1,3), 2,2-diethylpropane-diol-(1,3), hexanediol-(1,3), 1,4-di-(hydroxyethoxy)-benzene, 2,2-bis-(4-hydroxycyclohexyl)-propane, 2,4-dihydroxy-1,1,3,3-tetramethyl-cyclobutane, 2,2,4,4 tetramethylcyclobutanediol, 2,2-bis-(3-hydroxyethoxyphenyl)-propane, 2,2-bis-(4-hydroxypropoxyphenyl)-propane, isosorbide, hydroquinone, BDS-(2,2-(sulfonylbis)4,1-phenyleneoxy))bis(ethanol), and mixtures thereof.
43. The process of any one of claims 35 to 42 wherein said ester is poly(ethylene terephthalate).
44. The process of claim 40, 41 or 42 wherein said diacid or diacid generator are selected from the group consisting of terephthalic acid and dimethyl terephthalate, and said diol is ethylene glycol.
45. The process of any one of claims 35 to 39 wherein at least one of the pipe reactors has a means for recycling a portion of the process fluid, and the process comprises recycling a portion of the process fluid to the esterification pipe reactor.
46. The process of any one of claims 37 to 39 wherein at least one of the pipe reactors has a means for recycling a portion of the process fluid, and the process comprises recycling a portion of the process fluid to the polycondensation pipe reactor.
47. The process of claim 45 further comprising adding at least one reactant into the recycled process fluid.
48. The process of any one of claims 37, 38, or 39 wherein the polycondensation pipe reactor has a plurality of zones or stages and the process comprises operating at least two of the zones or stages at a pressure differential.
49. The process of any one of claims 35 to 39 further comprising removing a portion of the vapor from at least one of the pipe reactors.
50. The process of claim 49 comprising operating the esterification pipe reactor in a bubble or froth regime.
51. The process of claim 48 comprising operating the polycondensation pipe reactor in a stratified flow regime.
52. The process of claim 35 further including adding to the pipe reactor at least one material selected from a catalytic material, colorant, toner, pigment, carbon black, glass fiber, filler, impact modifier, antioxidant, stabilizer, flame retardant, reheat aid, acetaldehyde reducing compound, oxygen scavenging compound, UV absorbing compound, barrier improving additive, black iron oxide and mixtures thereof.
53. The process of claims 35 to 39, 50, or 51 wherein the pipe reactor is a substantially empty pipe.
54. The process of any one of claims 35 to 39 wherein the esterification pipe reactor is operated with a pressure profile between the first inlet and the first outlet and wherein the pressure at the first inlet is greater than the pressure at the first outlet.
55. The process of claim 54 wherein the pressure profile is established by a hydrostatic pressure inside the esterification pipe reactor.
56. The process of any one of claims 37 to 39 further comprising controlling the pressure between the esterification process and polycondensation process using a seal leg in fluid communication with and positioned between the esterification pipe reactor and the polycondensation pipe reactor.
57. The process of claim 56 further comprising heating the fluid in said seal leg.
58. The process of claim 57 wherein the fluid in the seal leg is heated to a boiling temperature.
59. The process of claim 49 further comprising recovering reactants from the removed vapor to form a reactant lean overhead product and a reactant rich bottom product.
60. The process of claim 49 further comprising oxidizing the removed vapor in an oxidizer selected from a heat transfer media furnace, an incinerator or a thermal oxidizer.
61. The process of claim 59 further comprising oxidizing the reactant lean overhead product in an oxidizer selected from a heat transfer media furnace, an incinerator or a thermal oxidizer.
62. The process of claim 59 further comprising recycling the reactant rich bottom product to the esterification pipe reactor.
63. The process of any one of claims 59-62 wherein at least one of said reactants is glycol.
64. The process of any one of claims 35 to 39 further comprising retrofitting said pipe reactor to a conventional polyester process having at least one continuous stirred tank reactor.
65. A process for making a polyester from a plurality of reactants comprising:
(a) providing an esterification pipe reactor having a first inlet and a first outlet;
(b) adding the reactants under esterification reaction conditions into the esterification pipe reactor proximate to the first inlet and forming a two phase flow so the reactants form a liquid phase and vapor phase flow through the esterification pipe reactor, 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 wherein at least a portion of the reactants form an ester monomer;
(c) reacting the monomer under polycondensation reaction conditions in a polycondensation pipe reactor wherein at least a portion of the ester monomer forms an oligomer; and (d) reacting the oligomer under polycondensation reaction conditions in the polycondensation pipe reactor wherein at least a portion of the oligomer forms a polyester.
66. An apparatus for preparing at least one ester monomer, ester oligomer or polyester comprising a pipe reactor having an inlet, an outlet and an interior through which reactants of at least one ester monomer, ester oligomer or polyester are passed wherein said reactants are reacted 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.
67. The apparatus of claim 66 wherein the pipe reactor is an esterification pipe reactor having a first inlet, a first outlet, a first inner surface and a first interior for passing reactants through.
68. The apparatus of claim 66 wherein the pipe reactor is a polycondensation pipe reactor having a second inlet, a second outlet, a second inner surface and a second interior for passing reactants through.
69. The apparatus of claim 66 wherein the pipe reactor comprises:
(a) an esterification pipe reactor having a first inlet, a first outlet, a first inner surface and a first interior for passing reactants through; and (b) a polycondensation pipe reactor having a second inlet, a second outlet, a second inner surface and a second interior for passing reactants through.
70. The apparatus of any one of claims 67 to 69 further comprising a fluid restricting means affixed to at least one of the inner surfaces.
71. The apparatus of claim 70 wherein the fluid restricting means comprises a weir for partially,blocking the flow of the fluids.
72. The apparatus of claim 69 wherein the second inlet and the first outlet are in fluid communication.
73. The apparatus of claim 67 or 69 wherein the first outlet is elevationally above the first inlet.
74. The apparatus of any one of claims 67 to 69 further comprising a means for recirculating at least a portion of fluid materials in at least one of the pipe reactors.
75. The apparatus of claim 67 or 69 further comprising a means for recirculating at least a portion of fluid materials, wherein the recirculating means comprises an influent and an effluent, and wherein the effluent is in fluid communication with the esterification pipe reactor.
76. The apparatus of claim 75 wherein the recirculating means effluent is located proximate to the first inlet of the esterification pipe reactor.
77. The apparatus of claims 66 to 69 or 71 further comprising a means for venting, degassing or removing vapors from at least a portion of the interior.
78. The apparatus of claim 77 wherein the venting or degassing means comprises at least one of:
(a) a linear stand pipe;
(b) a linear stand pipe having a liquid entrainment separator in-line with the vapor path;
(c) a non-linear stand pipe disposed vertically above the pipe reactor and formed of three contiguous sections each in fluid communication with the adjacent section, a substantially vertical first section in fluid communication with the pipe reactor, 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 that the third section is oriented substantially horizontally such that the non-linearity causes all or most of the liquid droplets in the vapor to impinge on some surface of the vent piping; or (d) a pressure decreasing device selected from an eductor, a siphon, an exhauster, a venturi nozzle, or a jet.
79. The apparatus of claim 68, 69 or 71 wherein the polycondensation reactor has a plurality of zones, stages or sections wherein a zone is defined by a relative pressure differential and wherein a seal leg is positioned between and in fluid communication with each zone, stage or section for controlling the pressure between reactor sections.
80. The apparatus of claim 71 wherein at least one pipe reactor comprises a flow inverter.
81. The apparatus of 80 wherein the flow inverter is proximate to and downstream of the weir.
82. The apparatus of claim 66 wherein the pipe reactor relative to a length has alternating linear and non-linear sections between the inlet and outlet thereof.
83. The apparatus of any one of claims 66 to 68 having a means for heating the reactants in the pipe reactor.
84. The apparatus of claim 83 wherein the heating means comprises at least one of:
(a) a jacket around an exterior surface of the pipe reactor which defines an annular space through which a heat transfer medium is circulated;
(b) a plurality of electrical heating components wrapped about the exterior surface of the pipe reactor; or (c) a heat exchanger along at least a portion of the pipe reactor whereby the reactants are passed to bring the temperature back up as the by-product vaporizes.
85. The apparatus of claim 84 wherein the heat transfer medium is selected from oil, water, vapor, or mixtures thereof.
86. The apparatus of any one of claims 66 to 68 wherein the pipe reactor is divided into a plurality of substantially parallel flow conduits extending between the inlet and the outlet thereof, and wherein the reactants flowing through the pipe reactor pass through at least one of the plurality of flow conduits while flowing through the reactor.
87. The apparatus of claim 84 wherein the heating means further comprises a heat transfer media control system having a supply heat transfer media loop through which a first stream of a heat transfer media is passed and a return heat transfer media loop through which a second stream of the heat transfer media is passed, the temperature of the first heat transfer media stream being greater than the temperature of the second heat transfer media stream, the heat transfer media control system including:
(a) a first heat transfer media header through which the first heat transfer media stream is passed;
(b) a second heat transfer media header through which the second heat transfer media stream is passed;
(c) a first heat transfer media sub-loop, through which the heat transfer media may be passed, from the first to the second headers, respectively;
(d) a control valve in fluid communication with a selected one of the headers and the first sub-loop;
wherein the pressure of the first heat transfer media stream within the first header being greater than the pressure of the second heat transfer media stream within the second header and the control valve is used to selectively direct at least a portion of the first heat transfer media stream into the first sub-loop using the pressure of the first heat transfer media stream to pass the heat transfer media, and to also control the temperature and pressure of the heat transfer media stream being passed through the first sub-loop.
88. The apparatus of claim 87 further comprising:
(a) a second heat transfer media sub-loop formed separately of the first sub-loop and in fluid communication therewith; and (b) a second control valve in fluid communication with the second sub-loop;
wherein the second control valve selectively directs at least a portion of the first heat transfer media stream into the second sub-loop to control the temperature and the pressure of the heat transfer media being passed through the second sub-loop.
89. The apparatus of claim 66-69, 78, 82, 84 or 85 wherein said pipe reactor is a substantially empty pipe.
90. The apparatus of claim 72 further comprising a seal leg in fluid communication with and positioned between the esterification pipe reactor and the polycondensation pipe reactor for controlling the pressure between the esterification process and polycondensation process.
91. The apparatus of claim 90 wherein the seal leg comprises a means for heating fluid in the seal leg.
92. The apparatus of claim 91 wherein said heating means is a heat exchanger positioned adjacent to the seal leg.
93. The apparatus of claim 91 wherein said heating means is a heat exchanger positioned in line with the seal leg.
94. The apparatus of claim 77 further comprising a means for recovering reactants from the removed vapor to form a reactant lean overhead product and a reactant rich bottom product.
95. The apparatus of claim 94 wherein said recovery means comprises at least one of a water column, a stripper column or a mixed glycol and monomer column.
96. The apparatus of claim 94 further comprising a means for oxidizing reactant lean overhead product wherein the oxidizer is selected from a heat transfer media furnace, an incinerator or a thermal oxidizer.
97. The apparatus of claim 77 further comprising means for oxidizing reactant lean overhead product wherein the oxidizer is selected from a heat transfer media furnace, an incinerator or a thermal oxidizer.
98. The apparatus of claim 66-69, 72, 78, 80, 87, 90 or 94 wherein said pipe reactor is retrofitted to a conventional polyester process having at least one continuous stirred tank reactor.
99. The process of claim 35 or claim 49 wherein said esterification pipe reactor is operated in the plug flow regime.
100. The process of claim 49 wherein said esterification pipe reactor is operated in the stratified flow regime.
101. The process of claim 48 wherein said polycondensation pipe reactor is operated in the plug flow regime.
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