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WO1999015268A1 - Pipe reactor - Google Patents

Pipe reactor Download PDF

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Publication number
WO1999015268A1
WO1999015268A1 PCT/US1998/019736 US9819736W WO9915268A1 WO 1999015268 A1 WO1999015268 A1 WO 1999015268A1 US 9819736 W US9819736 W US 9819736W WO 9915268 A1 WO9915268 A1 WO 9915268A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
polymer
lining
diameter
circulating tube
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1998/019736
Other languages
French (fr)
Inventor
Tadeusz Piotr Rygas
Kevin Robert Benson
Jeffrey Warren Mckown
Hsueh Sung Tung
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Honeywell International Inc
Original Assignee
AlliedSignal Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by AlliedSignal Inc filed Critical AlliedSignal Inc
Priority to AU94023/98A priority Critical patent/AU9402398A/en
Publication of WO1999015268A1 publication Critical patent/WO1999015268A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2435—Loop-type reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/02—Apparatus characterised by being constructed of material selected for its chemically-resistant properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B01J19/246—Stationary reactors without moving elements inside provoking a loop type movement of the reactants internally, i.e. the mixture circulating inside the vessel such that the upward stream is separated physically from the downward stream(s)
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
    • C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
    • C07C17/202—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction
    • C07C17/206—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction the other compound being HX
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/02—Apparatus characterised by their chemically-resistant properties
    • B01J2219/0204—Apparatus characterised by their chemically-resistant properties comprising coatings on the surfaces in direct contact with the reactive components
    • B01J2219/0245—Apparatus characterised by their chemically-resistant properties comprising coatings on the surfaces in direct contact with the reactive components of synthetic organic material
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the invention relates to apparatuses useful for reactions carried out under corrosive conditions.
  • the invention provides a polymer-lined pipe reactor useful for carrying out corrosive reactions, such as halogen exchange reactions.
  • Reactors used for corrosive media are usually glass-lined or made from corrosion resistant alloys such as INCONEL®, MONEL®, or HASTELLOY®. These materials are suitable for use for most reactions performed in chemical manufacturing. However, glass-lined equipment may not be suitable for use in certain reactions, for example fluorination reactions using hydrogen fluoride, because the reactants may attack the glass lining. Additionally, a number of industrially important reactions create extremely corrosive reaction media capable of destroying the corrosion resistant alloys.
  • the reactions' corrosivity results from the use of antimony halide catalysts and hydrogen fluoride.
  • antimony halide catalysts and hydrogen fluoride form corrosive super-acids.
  • the corrosion resistant alloys are corroded quickly in the presence of the super acids
  • PTFE polyterafluoroethylene polymer
  • PFTE- lined reactors are difficult to manufacture because the PFTE liner has a thermal expansion coefficient much larger than metal. This difference in thermal expansion coefficients has only a small effect at low reactor diameters because small deformations of PFTE are reversible. However, the effect becomes significant at diameters greater than 3 to 4 feet because the thermal deformations are so large that the PFTE liner may partially collapse.
  • PFTE-lined equipment with a diameter greater than 12 inches is generally not suitable for vacuum service because the liner stability decreases markedly with an increase in the diameter. Therefore, a need exists for a reactor that may be used for corrosive reactions, but that overcomes the problems associated with currently available reactors.
  • FIG. 1 is a schematic diagram of one embodiment of the apparatus of the invention.
  • Fig. 2 is a schematic diagram of another embodiment of the apparatus of the invention.
  • the present invention provides a pipe reactor for carrying out corrosive reactions, including fluorination reactions, which reactor overcomes some of the disadvantages of the currently available reactors. Additionally, the reactor of the invention provides a heat exchange surface that is larger than standard reactors.
  • the reactor of the invention comprises a polymer-lined pipe reactor having disposed therein or external thereto at least one circulating tube.
  • the reactor of the invention permits a large reactor volume at diameters of 3 ft or less because the length of the reactor may be made sufficiently long to obtain a large volume.
  • the polymer lining permits the use of the reactor with corrosive reaction materials.
  • the reactor of the invention is more easily constructed than standard polymer-lined reactors because the diameter of the reactor of the invention may be smaller than that of the standard reactor.
  • the reactor of the invention generally has a length to inside diameter ratio of about 4: 1 to about 100: 1, preferably about 4: 1 to about 50: 1, more preferably about 8:1 to about 20:1. This ratio allows for a heat exchange surface and reactor volume larger than that found on the standard polymer-lined reactor.
  • the residence time of the fluid in the reactor is a function of the volumetric flow rate through the reactor as well as the reactor length and diameter, which may be varied to achieve an optimum yield or selectivity for the desired product.
  • the inside diameter of the reactor is about 3 feet or less.
  • the reactor may be horizontally, vertically, or inclinedly disposed.
  • reactor 10 vertically disposed tubular reactor 10 is shown, which reactor is made of reactor shell 11 having a thickness of about 1/8 to about 2 inches, preferably about 1/8 to about 1.5 inches, which reactor shell 11 has an outer surface 12 and inner surface 13.
  • Reactor shell 11 may be constructed of any suitable material such as carbon steel, stainless steel, INCOLOY®, INCONEL®, HASTELLOY®, or the like.
  • Reactor 10 is polymer- lined meaning that inner surface 13 is coated, or lined, by any conventional means with polymer lining 14.
  • Polymer lining 14 may be any suitable corrosion resistant, fluorinated polymer, including without limitation, polytetrafluoroethylene (“PTFE”), perfluoroalkoxy polymer, ethylene tetrafluoroethylene polymer, vinylidene fluoride polymer, ethylene hexafluoropropylene polymer, and the like.
  • PTFE polytetrafluoroethylene
  • Polymer lining 14 may be of any desired thickness, but generally will be from about 1/8 to about 1/2 inch thick, preferably from about 1/4 to about 1/2 inch thick. Most preferably, polymer lining 14 is about 1/4 inch thick. All of the components of the reactor of the invention are constructed of suitable corrosion resistant materials.
  • the wetted components are made of fluorinated polymer, more preferably PTFE.
  • circulating tube 17 Disposed within reactor shell 11 is at least one circulating tube 17 located in the bottom two-thirds of tubular reactor 10.
  • the walls of circulating tube 17 are sufficiently thick to prevent a buckling of the tube.
  • the wall of circulating tube 17 may be up to about 1 inch thick and the tube may be of any convenient diameter, but preferably is of a diameter that is about 1/3 the diameter of the inside diameter of the reactor.
  • Circulating tube 17 is held in position within reactor shell 11 by a means for holding circular tube 17 vertically within reactor shell 11.
  • the holding means 19 is a plurality of spacers located between polymer lining 14 and circulating tube wall outer inner surface 21. Polymer lining 14 and circulating tube outer surface 21 define inner space 22. Inner space 22 below liquid level line 16 provides an area within which the reaction materials may react.
  • Circulating tube 17 is open meaning that circulating tube bottom 25 contains one or more openings that permit liquid from space 22 to flow into circulating tube 17.
  • flow through circulating tube 17 is in the upward direction. In another embodiment, the flow is reversed and liquid flows out of circulating tube bottom 25. Circulating tube 17 achieves mixing without the use of a mechanical agitator or external circulating pump.
  • the reaction materials mix and circulate within pipe reactor 21 as a result of the hydrostatic pressures inside and outside of circulating tube 17.
  • Reaction materials are charged to tubular reactor 10 through a means for feeding 26, which means may be any convenient means for feeding reaction materials, such as a sparger or a feeding line.
  • Feeding tube 27, fully or partially disposed within circulating tube 17, is connected to feeding means 26 at its lower end 29. Feeding means 26 may be situated inside or outside of circulating tube 17.
  • feeding means 26 is within circulating tube 17, the flow inside of feeding tube 27 will be upward and if outside, the flow will be in the downward direction.
  • the use of a circulating tube permits mixing of the reaction materials without the use of an agitator because the reaction mixture continuously circulates in the reactor due to the flow in the circulating tube, which flow results from differences in the hydrostatic pressure inside and outside of the tube. Such mixing results in an increase in productivity per unit volume.
  • FIG. 2 another embodiment, horizontally disposed reactor
  • Reactor 20 is shown having reactor shell 39 and polymer lining 41.
  • Reactor 20 is suitable for use in two phase reactions, including those in which the formation of a suspension is difficult.
  • Reactor 20 may have an circulating tube that is internally or externally disposed to reactor shell 39.
  • the horizontally disposed reactor circulating tube is externally disposed.
  • Feeding tube 36 and circulating tube 33 are connected to reactor shell 39 by any convenient, means known in the art. Reaction materials are fed via feeding inlet 37 and feeding means 35, which may be any known feeding means such as a sparger, into circulating tube 33 and feeding tube 36. Following reaction, a product stream exits via outlet 42.
  • the reactor of the invention is beneficial because it requires only small diameter polymer-lined pipes to manufacture.
  • the reactor is constructed as a segmented reactor to accommodate differences in thermal expansion between the polymer-lining and the reactor outer shell.
  • the reactor of the invention will be useful in any number of highly corrosive reactions, it may find its greatest utility in carrying out liquid phase, halogen exchange reactions in which the starting materials are an organic feed and hydrogen fluoride and which use a halogenated antimony catalyst.
  • the invention provides a liquid phase, halogen exchange reaction comprising providing the reactor of the invention and carrying out the halogen exchange reaction within the reactor. Such reactions typically are carried out at greater than about 90° C and pressures below about 300 psig.
  • Suitable organic feed materials for such reactions are any hydrocarbon, chlorofluorocarbon, hydrochlorofluorocarbon, or hydrofluorocarbon that can be fluorinated; that is, the organic feed may be any such material containing a carbon- bonded chlorine or other atom replaceable by fluorine and/or that may contain carbon-carbon bond unsaturation saturatable with fluorine.
  • suitable organic materials include, without limitation, halogenopropanes, chloroethanes, chloromethanes, and chlorobutanes.
  • Any suitable fluorination catalyst may be used including, without limitation, titanium, tin, niobium, and tantalum halide catalyst.
  • antimony halide catalysts such antimony pentachloride will be used.
  • concentration of organic feed to hydrogen fluoride used may be determined by one ordinarily skilled in the art based on a number of considerations including, without limitation, stoichiometric amounts needed to replace the desired number of atoms in the organic feed, amounts needed to fluorinate the catalyst, and amounts needed to provide an excess of hydrofluoric acid.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

An apparatus useful for reactions carried out under corrosive conditions is provided. In particular, a polymer-lined pipe reactor (10, 20) with an internal (17) or external circulating tube (33) useful for carrying out corrosive reactions, such as halogen exchange reactions, is provided.

Description

PIPE REACTOR Field of the Invention The invention relates to apparatuses useful for reactions carried out under corrosive conditions. In particular, the invention provides a polymer-lined pipe reactor useful for carrying out corrosive reactions, such as halogen exchange reactions.
Background of the Invention Reactors used for corrosive media are usually glass-lined or made from corrosion resistant alloys such as INCONEL®, MONEL®, or HASTELLOY®. These materials are suitable for use for most reactions performed in chemical manufacturing. However, glass-lined equipment may not be suitable for use in certain reactions, for example fluorination reactions using hydrogen fluoride, because the reactants may attack the glass lining. Additionally, a number of industrially important reactions create extremely corrosive reaction media capable of destroying the corrosion resistant alloys.
In the case of halogen exchange reactions, the reactions' corrosivity results from the use of antimony halide catalysts and hydrogen fluoride. Specifically, antimony halide catalysts and hydrogen fluoride form corrosive super-acids. At high catalyst concentrations, or concentrations greater than about 35 weight percent of the antimony halide catalyst, and temperatures above 90° C, the corrosion resistant alloys are corroded quickly in the presence of the super acids
One proposed solution to the corrosion problem is the use of polyterafluoroethylene polymer ("PTFE") lining in the reactor. However, PTFE- lined reactors are difficult to manufacture because the PFTE liner has a thermal expansion coefficient much larger than metal. This difference in thermal expansion coefficients has only a small effect at low reactor diameters because small deformations of PFTE are reversible. However, the effect becomes significant at diameters greater than 3 to 4 feet because the thermal deformations are so large that the PFTE liner may partially collapse. Additionally, PFTE-lined equipment with a diameter greater than 12 inches is generally not suitable for vacuum service because the liner stability decreases markedly with an increase in the diameter. Therefore, a need exists for a reactor that may be used for corrosive reactions, but that overcomes the problems associated with currently available reactors.
Brief Description of the Drawings Fig. 1 is a schematic diagram of one embodiment of the apparatus of the invention.
Fig. 2 is a schematic diagram of another embodiment of the apparatus of the invention.
Description of the Invention and Preferred Embodiments The present invention provides a pipe reactor for carrying out corrosive reactions, including fluorination reactions, which reactor overcomes some of the disadvantages of the currently available reactors. Additionally, the reactor of the invention provides a heat exchange surface that is larger than standard reactors.
The reactor of the invention comprises a polymer-lined pipe reactor having disposed therein or external thereto at least one circulating tube. The reactor of the invention permits a large reactor volume at diameters of 3 ft or less because the length of the reactor may be made sufficiently long to obtain a large volume. Additionally, the polymer lining permits the use of the reactor with corrosive reaction materials. Further, the reactor of the invention is more easily constructed than standard polymer-lined reactors because the diameter of the reactor of the invention may be smaller than that of the standard reactor.
The reactor of the invention generally has a length to inside diameter ratio of about 4: 1 to about 100: 1, preferably about 4: 1 to about 50: 1, more preferably about 8:1 to about 20:1. This ratio allows for a heat exchange surface and reactor volume larger than that found on the standard polymer-lined reactor.
The residence time of the fluid in the reactor is a function of the volumetric flow rate through the reactor as well as the reactor length and diameter, which may be varied to achieve an optimum yield or selectivity for the desired product. Preferably, the inside diameter of the reactor is about 3 feet or less. The reactor may be horizontally, vertically, or inclinedly disposed.
Referring to Fig. 1, one embodiment of the invention, vertically disposed tubular reactor 10 is shown, which reactor is made of reactor shell 11 having a thickness of about 1/8 to about 2 inches, preferably about 1/8 to about 1.5 inches, which reactor shell 11 has an outer surface 12 and inner surface 13. Reactor shell 11 may be constructed of any suitable material such as carbon steel, stainless steel, INCOLOY®, INCONEL®, HASTELLOY®, or the like. Reactor 10 is polymer- lined meaning that inner surface 13 is coated, or lined, by any conventional means with polymer lining 14. Polymer lining 14 may be any suitable corrosion resistant, fluorinated polymer, including without limitation, polytetrafluoroethylene ("PTFE"), perfluoroalkoxy polymer, ethylene tetrafluoroethylene polymer, vinylidene fluoride polymer, ethylene hexafluoropropylene polymer, and the like. Preferably, PTFE polymer is used. Polymer lining 14 may be of any desired thickness, but generally will be from about 1/8 to about 1/2 inch thick, preferably from about 1/4 to about 1/2 inch thick. Most preferably, polymer lining 14 is about 1/4 inch thick. All of the components of the reactor of the invention are constructed of suitable corrosion resistant materials. Preferably, the wetted components are made of fluorinated polymer, more preferably PTFE.
Disposed within reactor shell 11 is at least one circulating tube 17 located in the bottom two-thirds of tubular reactor 10. The walls of circulating tube 17 are sufficiently thick to prevent a buckling of the tube. The wall of circulating tube 17 may be up to about 1 inch thick and the tube may be of any convenient diameter, but preferably is of a diameter that is about 1/3 the diameter of the inside diameter of the reactor. Circulating tube 17 is held in position within reactor shell 11 by a means for holding circular tube 17 vertically within reactor shell 11. Preferably, the holding means 19 is a plurality of spacers located between polymer lining 14 and circulating tube wall outer inner surface 21. Polymer lining 14 and circulating tube outer surface 21 define inner space 22. Inner space 22 below liquid level line 16 provides an area within which the reaction materials may react.
Base 23 of circulating tube 17 rests on at least one supporting means 24 so that base 23 does not rest on polymer lining 14. Circulating tube 17 is open meaning that circulating tube bottom 25 contains one or more openings that permit liquid from space 22 to flow into circulating tube 17.
In one embodiment, flow through circulating tube 17 is in the upward direction. In another embodiment, the flow is reversed and liquid flows out of circulating tube bottom 25. Circulating tube 17 achieves mixing without the use of a mechanical agitator or external circulating pump. The reaction materials mix and circulate within pipe reactor 21 as a result of the hydrostatic pressures inside and outside of circulating tube 17. Reaction materials are charged to tubular reactor 10 through a means for feeding 26, which means may be any convenient means for feeding reaction materials, such as a sparger or a feeding line. Feeding tube 27, fully or partially disposed within circulating tube 17, is connected to feeding means 26 at its lower end 29. Feeding means 26 may be situated inside or outside of circulating tube 17. If feeding means 26 is within circulating tube 17, the flow inside of feeding tube 27 will be upward and if outside, the flow will be in the downward direction. The use of a circulating tube permits mixing of the reaction materials without the use of an agitator because the reaction mixture continuously circulates in the reactor due to the flow in the circulating tube, which flow results from differences in the hydrostatic pressure inside and outside of the tube. Such mixing results in an increase in productivity per unit volume.
A product stream containing product, unreacted starting materials, reaction intermediates, and byproducts exits reactor 10 via outlet 31 for further processing. Reactor shell feed inlet 15, connected to upper end 32 of feeding tube 27, receives recycle from such processing, which recycle contains unreacted starting materials and reaction intermediates.
Referring now to Fig. 2, another embodiment, horizontally disposed reactor
20 is shown having reactor shell 39 and polymer lining 41. Reactor 20 is suitable for use in two phase reactions, including those in which the formation of a suspension is difficult. Reactor 20 may have an circulating tube that is internally or externally disposed to reactor shell 39. Preferably, the horizontally disposed reactor circulating tube is externally disposed. The external circulating tube is disposed to reactor shell 39 at an angle of about γ = atan(D/sqrt(L2 + D2) where L is the reactor length and D is reactor diameter. Feeding tube 36 and circulating tube 33 are connected to reactor shell 39 by any convenient, means known in the art. Reaction materials are fed via feeding inlet 37 and feeding means 35, which may be any known feeding means such as a sparger, into circulating tube 33 and feeding tube 36. Following reaction, a product stream exits via outlet 42.
The reactor of the invention is beneficial because it requires only small diameter polymer-lined pipes to manufacture. Preferably, the reactor is constructed as a segmented reactor to accommodate differences in thermal expansion between the polymer-lining and the reactor outer shell.
Although the reactor of the invention will be useful in any number of highly corrosive reactions, it may find its greatest utility in carrying out liquid phase, halogen exchange reactions in which the starting materials are an organic feed and hydrogen fluoride and which use a halogenated antimony catalyst. Thus, in yet another embodiment, the invention provides a liquid phase, halogen exchange reaction comprising providing the reactor of the invention and carrying out the halogen exchange reaction within the reactor. Such reactions typically are carried out at greater than about 90° C and pressures below about 300 psig.
Suitable organic feed materials for such reactions are any hydrocarbon, chlorofluorocarbon, hydrochlorofluorocarbon, or hydrofluorocarbon that can be fluorinated; that is, the organic feed may be any such material containing a carbon- bonded chlorine or other atom replaceable by fluorine and/or that may contain carbon-carbon bond unsaturation saturatable with fluorine. Representative examples of suitable organic materials include, without limitation, halogenopropanes, chloroethanes, chloromethanes, and chlorobutanes.
Any suitable fluorination catalyst may be used including, without limitation, titanium, tin, niobium, and tantalum halide catalyst. Preferably, antimony halide catalysts, such antimony pentachloride will be used. The concentration of organic feed to hydrogen fluoride used may be determined by one ordinarily skilled in the art based on a number of considerations including, without limitation, stoichiometric amounts needed to replace the desired number of atoms in the organic feed, amounts needed to fluorinate the catalyst, and amounts needed to provide an excess of hydrofluoric acid.

Claims

What is claimed is:
1. A reaction apparatus comprising a polymer-lined pipe reactor having disposed therein or external thereto at least one circulating tube.
2. The apparatus of claim 1 wherein the pipe reactor has a diameter of about 3 feet or less.
3. The apparatus of claim 1 wherein the ratio of the reactor length to inside diameter is about 4: 1 to about 100: 1.
4. The apparatus of claim 1 wherein the ratio of the reactor length to inside diameter is about 8: 1 to about 20:1.
5. The apparatus of claim 1 wherein the reactor polymer lining is polytetrafluoroethylene, perfluoroalkoxy polymer, ethylene tetrafluoroethylene polymer, vinylidene fluoride polymer, or ethylene hexafluoropropylene polymer.
6. The apparatus of claim 1 wherein the reactor polymer lining is polytetrafluoroethylene polymer.
7. A reaction apparatus comprising a polymer-lined pipe reactor having disposed therein at least one circulating tube.
8. The apparatus of claim 7 wherein the pipe reactor has a diameter of about 3 feet or less.
9. The apparatus of claim 7 wherein the ratio of the reactor length to inside diameter is about 4:1 to about 100:1.
10. The apparatus of claim 7 wherein the ratio of the reactor length to inside diameter is about 8:1 to about 20:1.
11. The apparatus of claim 7 wherein the reactor polymer lining is polytetrafluoroethylene, perfluoroalkoxy polymer, ethylene tetrafluoroethylene polymer, vinylidene fluoride polymer, or ethylene hexafluoropropylene polymer.
12. The apparatus of claim 7 wherein the reactor polymer lining is polytetrafluoroethylene polymer.
13. A reaction apparatus comprising a polymer-lined pipe reactor having at least one circulating tube externally disposed thereto at an angle of about γ = atan(D/sqrt(L2 + D2) wherein L is the reactor length and D is reactor diameter.
14. The apparatus of claim 13 wherein the pipe reactor has a diameter of about 3 feet or less.
15. The apparatus of claim 13 wherein the ratio of the reactor length to inside diameter is about 4: 1 to about 100: 1.
16. The apparatus of claim 13 wherein the ratio of the reactor length to inside diameter is about 8: 1 to about 20:1.
17. The apparatus of claim 13 wherein the reactor polymer lining is polytetrafluoroethylene, perfluoroalkoxy polymer, ethylene tetrafluoroethylene polymer, vinylidene fluoride polymer, or ethylene hexafluoropropylene polymer.
18. The apparatus of claim 13 wherein the reactor polymer lining is polytetrafluoroethylene polymer.
19. A liquid phase halogen exchange reaction comprising the steps of:
(a) providing the apparatus of claims 1, 7, or 13; and
(b) carrying out the reaction in the reactor.
PCT/US1998/019736 1997-09-22 1998-09-22 Pipe reactor Ceased WO1999015268A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU94023/98A AU9402398A (en) 1997-09-22 1998-09-22 Pipe reactor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US93519997A 1997-09-22 1997-09-22
US08/935,199 1997-09-22

Publications (1)

Publication Number Publication Date
WO1999015268A1 true WO1999015268A1 (en) 1999-04-01

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150225316A1 (en) * 2014-02-10 2015-08-13 Daniel C. Merkel Reactor for liquid phase fluorination reactions
CN110790632A (en) * 2019-10-09 2020-02-14 江苏三美化工有限公司 Method for producing fluorinated alkane through liquid phase method pipelining continuous separation
CN110790633A (en) * 2019-10-09 2020-02-14 浙江大学 A method for the production of R32 and R31 by liquid-phase pipeline polyproduction

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE804724C (en) * 1947-03-20 1951-04-30 Solvay Process and device for continuous polymerisation
US4131742A (en) * 1975-11-03 1978-12-26 Bp Chemicals Limited Cobalt-catalyzed oxidation of hydrocarbons
US4166536A (en) * 1977-03-16 1979-09-04 The Carborundum Company Corrosive chemical containment system
EP0460735A2 (en) * 1990-06-04 1991-12-11 ENICHEM SYNTHESIS S.p.A. Process for producing dimethyl carbonate
EP0729932A1 (en) * 1995-03-03 1996-09-04 Central Glass Company, Limited Method of producing halopropane

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE804724C (en) * 1947-03-20 1951-04-30 Solvay Process and device for continuous polymerisation
US4131742A (en) * 1975-11-03 1978-12-26 Bp Chemicals Limited Cobalt-catalyzed oxidation of hydrocarbons
US4166536A (en) * 1977-03-16 1979-09-04 The Carborundum Company Corrosive chemical containment system
EP0460735A2 (en) * 1990-06-04 1991-12-11 ENICHEM SYNTHESIS S.p.A. Process for producing dimethyl carbonate
EP0729932A1 (en) * 1995-03-03 1996-09-04 Central Glass Company, Limited Method of producing halopropane

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150225316A1 (en) * 2014-02-10 2015-08-13 Daniel C. Merkel Reactor for liquid phase fluorination reactions
US9353028B2 (en) * 2014-02-10 2016-05-31 Honeywell International Inc. Reactor for liquid phase fluorination reactions
CN110790632A (en) * 2019-10-09 2020-02-14 江苏三美化工有限公司 Method for producing fluorinated alkane through liquid phase method pipelining continuous separation
CN110790633A (en) * 2019-10-09 2020-02-14 浙江大学 A method for the production of R32 and R31 by liquid-phase pipeline polyproduction

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Publication number Publication date
AU9402398A (en) 1999-04-12

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