US20020022753A1 - Process for dehydrohalogenation of halog enated compounds - Google Patents
Process for dehydrohalogenation of halog enated compounds Download PDFInfo
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- US20020022753A1 US20020022753A1 US09/801,142 US80114201A US2002022753A1 US 20020022753 A1 US20020022753 A1 US 20020022753A1 US 80114201 A US80114201 A US 80114201A US 2002022753 A1 US2002022753 A1 US 2002022753A1
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- 150000001875 compounds Chemical class 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims description 52
- 238000006704 dehydrohalogenation reaction Methods 0.000 title claims description 20
- MUQNGPZZQDCDFT-JNQJZLCISA-N Halcinonide Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@]2(F)[C@@H]1[C@@H]1C[C@H]3OC(C)(C)O[C@@]3(C(=O)CCl)[C@@]1(C)C[C@@H]2O MUQNGPZZQDCDFT-JNQJZLCISA-N 0.000 title 1
- 229940028332 halog Drugs 0.000 title 1
- 238000013019 agitation Methods 0.000 claims abstract description 13
- 238000009835 boiling Methods 0.000 claims abstract description 10
- 238000009834 vaporization Methods 0.000 claims abstract description 3
- 230000008016 vaporization Effects 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 40
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 30
- 238000006243 chemical reaction Methods 0.000 claims description 30
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 19
- 150000001336 alkenes Chemical class 0.000 claims description 18
- 238000002156 mixing Methods 0.000 claims description 18
- 239000007791 liquid phase Substances 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- 239000007864 aqueous solution Substances 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 4
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical class C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 claims description 2
- 125000000383 tetramethylene group Chemical class [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 2
- 239000003960 organic solvent Substances 0.000 claims 1
- 239000000376 reactant Substances 0.000 abstract description 24
- 238000011065 in-situ storage Methods 0.000 abstract description 2
- 239000007795 chemical reaction product Substances 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- 239000000047 product Substances 0.000 description 15
- 239000002585 base Substances 0.000 description 13
- YACLQRRMGMJLJV-UHFFFAOYSA-N chloroprene Chemical compound ClC(=C)C=C YACLQRRMGMJLJV-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 11
- 229910052751 metal Inorganic materials 0.000 description 11
- 239000002184 metal Substances 0.000 description 11
- 229910001868 water Inorganic materials 0.000 description 10
- XVEASTGLHPVZNA-UHFFFAOYSA-N 3,4-dichlorobut-1-ene Chemical compound ClCC(Cl)C=C XVEASTGLHPVZNA-UHFFFAOYSA-N 0.000 description 7
- 239000008346 aqueous phase Substances 0.000 description 7
- 239000012074 organic phase Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- -1 alkali metal alkoxides Chemical class 0.000 description 5
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 5
- 150000003841 chloride salts Chemical class 0.000 description 4
- 150000002896 organic halogen compounds Chemical class 0.000 description 4
- 239000003444 phase transfer catalyst Substances 0.000 description 4
- 239000011541 reaction mixture Substances 0.000 description 4
- GVEUEBXMTMZVSD-UHFFFAOYSA-N 3,3,4,4,5,5,6,6,6-nonafluorohex-1-ene Chemical group FC(F)(F)C(F)(F)C(F)(F)C(F)(F)C=C GVEUEBXMTMZVSD-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000000977 initiatory effect Effects 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- JZNOXYXRJDVNOM-UHFFFAOYSA-N 1,1,1,2,2,3,3,4,4,5,6,6,6-tridecafluoro-5-iodohexane Chemical compound FC(F)(F)C(F)(F)C(F)(F)C(F)(F)C(F)(I)C(F)(F)F JZNOXYXRJDVNOM-UHFFFAOYSA-N 0.000 description 2
- UAZUEJTXWAXSMA-UHFFFAOYSA-N 1,1-dichlorobut-1-ene Chemical compound CCC=C(Cl)Cl UAZUEJTXWAXSMA-UHFFFAOYSA-N 0.000 description 2
- ASHCDEYFCNWSTR-UHFFFAOYSA-N 1,4-dibromo-1,1,2,2-tetrafluorobutane Chemical compound FC(F)(Br)C(F)(F)CCBr ASHCDEYFCNWSTR-UHFFFAOYSA-N 0.000 description 2
- WZUZDBPJFHQVJC-UHFFFAOYSA-N 2,3,4-trichlorobut-1-ene Chemical compound ClCC(Cl)C(Cl)=C WZUZDBPJFHQVJC-UHFFFAOYSA-N 0.000 description 2
- LIFLRQVHKGGNSG-UHFFFAOYSA-N 2,3-dichlorobuta-1,3-diene Chemical compound ClC(=C)C(Cl)=C LIFLRQVHKGGNSG-UHFFFAOYSA-N 0.000 description 2
- GVCWGFZDSIWLMO-UHFFFAOYSA-N 4-bromo-3,3,4,4-tetrafluorobut-1-ene Chemical compound FC(F)(Br)C(F)(F)C=C GVCWGFZDSIWLMO-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-N Hydrogen bromide Chemical compound Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 235000019270 ammonium chloride Nutrition 0.000 description 2
- 239000003125 aqueous solvent Substances 0.000 description 2
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 125000005843 halogen group Chemical group 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 239000010815 organic waste Substances 0.000 description 2
- 125000001453 quaternary ammonium group Chemical group 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- GETQZCLCWQTVFV-UHFFFAOYSA-N trimethylamine Chemical compound CN(C)C GETQZCLCWQTVFV-UHFFFAOYSA-N 0.000 description 2
- 125000003837 (C1-C20) alkyl group Chemical group 0.000 description 1
- XFNJYAKDBJUJAJ-UHFFFAOYSA-N 1,2-dibromopropane Chemical compound CC(Br)CBr XFNJYAKDBJUJAJ-UHFFFAOYSA-N 0.000 description 1
- QBGVARBIQGHVKR-UHFFFAOYSA-N 1,3-dichlorobutane Chemical compound CC(Cl)CCCl QBGVARBIQGHVKR-UHFFFAOYSA-N 0.000 description 1
- OVJCTKGXZMKBCX-UHFFFAOYSA-N 1-bromo-3,3,4,4-tetrafluorobut-1-ene Chemical group FC(F)C(F)(F)C=CBr OVJCTKGXZMKBCX-UHFFFAOYSA-N 0.000 description 1
- NIDSRGCVYOEDFW-UHFFFAOYSA-N 1-bromo-4-chlorobutane Chemical compound ClCCCCBr NIDSRGCVYOEDFW-UHFFFAOYSA-N 0.000 description 1
- WJSVHHICQPRGSM-UHFFFAOYSA-N 2-chloro-1-iodobutane Chemical compound CCC(Cl)CI WJSVHHICQPRGSM-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 125000003358 C2-C20 alkenyl group Chemical group 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 241000220317 Rosa Species 0.000 description 1
- 125000004067 aliphatic alkene group Chemical class 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 125000003342 alkenyl group Chemical group 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007033 dehydrochlorination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 125000001033 ether group Chemical group 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910000042 hydrogen bromide Inorganic materials 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 125000004433 nitrogen atom Chemical group N* 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 150000003856 quaternary ammonium compounds Chemical class 0.000 description 1
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- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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- FQDIANVAWVHZIR-OWOJBTEDSA-N trans-1,4-Dichlorobutene Chemical compound ClC\C=C\CCl FQDIANVAWVHZIR-OWOJBTEDSA-N 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
-
- 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
- This invention relates to an improved process for production of alkenes from halogenated organic compounds. More specifically, this invention relates to a process for dehydrohalogenation of halogenated organic compounds using a staged upflow reactor.
- Dehydrohalogenation of halogenated organic compounds is generally conducted in the liquid phase by mixing a halogenated alkane or halogenated alkene with a strong base in a solvent. Because the base is usually added as an aqueous solution, phase transfer catalysts are often employed to promote contact of the reactants.
- the present invention is directed to an improved process for dehydrohalogenation of organic compounds.
- the present invention relates to a process for dehydrohalogenation of a halogenated compound selected from the group consisting of halogenated alkanes and halogenated alkenes, said process comprising
- FIG. 1 is a schematic diagram of one embodiment of the process of the present invention.
- the dehydrohalogenation process of the present invention takes place in the liquid phase in a staged bubble reactor.
- Bubble reactors are extensively used in the chemical industry and consist of a contact region in which a discontinuous gas phase in the form of bubbles moves relative to a continuous phase.
- Bubble reactors can be single staged or multistaged, single channel or multi-channel, batch or continuous.
- a preferred type of bubble reactor is a co-current vertical column containing multiple stages, hereinafter referred to as a multi-staged upflow reactor.
- the halogenated organic compound or compounds that serve as the reactants may be selected from the group consisting of halogenated aliphatic alkanes or halogenated aliphatic alkenes.
- Preferred compounds are those having two to eight carbon atoms. Any saturated or unsaturated halogenated alkane or halogenated alkene that can be dehydrohalogenated with alkali is suitable for use in the process of the invention. These halogenated compounds will have at least one hydrogen atom. Fluorinated, chlorinated, brominated or iodinated alkanes or alkenes are all suitable reactants.
- Preferred halogenated compound reactants are chlorinated butadienes or chlorinated butenes.
- the halogenated alkanes or alkenes may contain a single species of halogen atom or they may contain more than one type of halogen atom.
- the process is particularly useful for dehydrochlorination of chlorinated alkanes and chlorinated alkenes in the presence of aqueous alkali.
- Suitable halogenated alkanes or halogenated alkenes include 1,4-dichlorobutene-2; 3,4-dichlorobutene-1; 2,3,4-trichlorobutene-1; 2-chloro-3-bromobutene-1; 1,2-dibromopropane; 1,3-dichlorobutane; 1-iodo-2-chlorobutane; perfluorobutylethyliodide; and 1,4-dibromo-1,1,2,2-tetrafluorobutane.
- the halogenated reactant may be in the form of a solid, a liquid or a gas at ambient temperature. However, liquid halogenated alkanes or alkenes are preferred. In addition, the halogenated reactant must either be a liquid or be present in a liquid phase under the conditions at which the dehydrohalogenation reaction is conducted.
- the dehydrohalogenating agent which is a base having a K b of at least 10 ⁇ 9
- Suitable bases include pyridine, trimethylamine, ammonia, ammonium hydroxide, calcium hydroxide, alkali metal hydroxides, and alkali metal alkoxides.
- the base will have a K b of at least 10 ⁇ 5 , and most preferably the base will be completely ionized, as in the case of aqueous alkali. Any aqueous alkali metal hydroxide is suitable for purposes of the invention, but sodium hydroxide and potassium hydroxide are preferred.
- the alkali normally will be present in excess in the reaction mixture. Generally, a mole ratio of alkali to halogenated reactant will be approximately 1.01-2.00. The precise amount will be determined based on factors such as the type of catalyst used and the particular reactants.
- the reaction takes place in the liquid phase.
- the reaction mixture will normally contain at least one liquid.
- the halogenated reactants may be liquids under conditions of the reaction or they may be dissolved in aqueous or non-aqueous solvents. If the reactants are present as solutions, the solvents may be miscible or immiscible.
- the halogenated reactant is a liquid and an alkali metal hydroxide dehydrohalogenating agent is present as an aqueous solution.
- the dehydrohalogenation may take place in the presence of a non-aqueous solvent such as methanol, for example as disclosed in U.S. Pat. No. 4,104,316.
- a phase transfer catalyst is used to promote contact between the two immiscible liquids, i.e. the organic and aqueous phases.
- Preferred catalysts are quaternary ammonium salts, especially quaternary ammonium chlorides, particularly those represented by the formula R 1 R 2 R 3 R 4 NCl in which each of R 1 , R 2 and R 3 independently is a C 1 -C 20 alkyl, a C 2 -C 20 alkenyl, or a C 7 -C 20 aralkyl, and R 4 is a C 6 -C 20 alkyl or alkenyl, benzyl, or a (C 6 -C 20 ) alkyl- or alkenyl-substituted benzyl.
- Each of R 1 , R 2 , and R 3 groups in these quaternary ammonium chlorides may also contain a hydroxyl or ether group in a position beta to the nitrogen atom.
- the amount of the quaternary ammonium compound is generally about 0.01-10% by weight of the starting halogenated alkane or alkene.
- Other phase transfer catalysts include amine oxides, such as those disclosed in U.S. Pat. No. 3,876,716 and quaternary phosphonium compounds, such as those disclosed in U.S. Pat. No. 3,639,493.
- optional components may be present in the reaction mixture, for example inhibitors, stabilizers and dispersants.
- inhibitors for example inhibitors, stabilizers and dispersants.
- dispersants for example inhibitors, stabilizers and dispersants.
- the use of such optional components will depend on the nature of the reactants and products to be produced.
- the halogenated alkane or halogenated alkene, and the base are contacted in a bubble reactor in a liquid phase, thereby initiating an exothermic reaction to produce a dehydrohalogenated compound having a boiling point lower than that of the halogenated reactant.
- the heat liberated during the reaction vaporizes the dehydrohalogenated compound thus produced.
- the vaporized product and water vapor that forms as a result of the dehydrohalogenation constitutes the gaseous phase that provides agitation of the reaction mixture as it moves through the reactor. Consequently, no internal stirring device is necessary within the reactor.
- stirring means such as a mechanical stirrer, can be present, but the presence of such devices is not necessary. Because the reaction is exothermic, it is not necessary to supply external heat to the reactor. In some instances it is useful to supply a small amount of heat initially for purposes of initiating the reaction or for temperature control.
- the reactor is a multi-stage type, preferably having at least three stages, most preferably 4-20 stages. Reactors having only one stage provide low single pass conversion. Consequently, separation and recycle of the unconverted reactants must be undertaken which increases complexity and cost of the process when used on an industrial scale.
- the reactor will be a vertical column reactor because it greatly simplifies flow from stage to stage. That is, when an upflow reactor is employed, liquid reactants are entrained up through the stages by the rising bubbles. This eliminates the need for pumps to transfer reactants from stage to stage.
- the process of the present invention can take place in a series of continuous, distinct tanks or vessels.
- chlorinated alkane or chlorinated alkene reactant and aqueous alkali metal hydroxide will be pre-mixed before introduction to the reactor.
- mixing devices include tanks fitted with mechanical agitators, that is stirred tank reactors, continuous stirred tank reactors, pumps and motionless stationary mixers. Reaction is initiated in the mixing device. This exothermic reaction provides heat and raises the vapor pressure to the point where some evaporation occurs upon entry to the bubble reactor.
- Mixing devices that are particularly useful in the practice of the invention include homogenizers, colloid mills, stirred tank reactors and centrifugal pumps.
- Prior art bubble reactor processes typically involve introduction of a single gas phase and a single liquid phase to the reactor.
- Other variations include the combination of a gas phase plus a solid phase or a three phase process involving a liquid, gas and a solid phase, i.e. a slurry.
- Such processes are discussed by Y. T. Shah, et al. in Design Parameters Estimations for Bubble Column Reactors , American Institute of Chemical Engineers Journal, 28, No. 3, 353 (1982) and S. Lee and Y. Tsui, Succeed at Gas/Liquid Contacting , Chemical Engineering Progress, 23 (July 1999). In the present process two liquids, but no gases, are fed to the system.
- the gas which is necessary for functioning of the bubble reactor, is generated in situ by the present process.
- This provides an agitation means for the bubble reactor, preferably the primary means of agitation, thereby decreasing the complexity of the process and increasing overall efficiency.
- Mass transfer from the gas to the liquid is not a factor that influences the reaction.
- the gas is a working fluid that controls temperature by its formation and provides agitation by virtue of its buoyancy. Further, the gas formation greatly enhances the kinetic efficiency of the reaction.
- the process of the present invention is useful for production of a wide variety of dehydrohalogenated products, for example, 2-methyl-3-chloropropene-1; 2-bromopropene-1; 3-chlorobutene-2; 2,3-dichloro-1-3-butadiene; perfluorobutylethylene; and 4-bromo-3,3,4,4-tetrafluorobutene. It is particularly useful in production of chloroprene from 3,4-dichlorobutene-2.
- the process of the present invention enhances the kinetics of the dehydrohalogenation process. That is, it promotes concentration of the catalyst and reactants, due to evaporation of the product, thus resulting in an increase in reaction rate.
- the process is most effective when the boiling point of the base used is between that of the dehydrohalogenated product and the organic reactant.
- the boiling point of the base will be that of the aqueous base solution, under the particular reaction conditions.
- 3,4-dichlorobutene-1 can be dehydrohalogenated to form chloroprene in the presence of 22 wt. % aqueous sodium hydroxide according to the present invention.
- the boiling point of water in a 22 wt. % aqueous sodium hydroxide solution is 110°-111° C. Under the temperature and pressure conditions of the reaction, the boiling points of chloroprene and 3,4-dichlorobutene-1 are 59° C. and 126° C., respectively. The yield of product under these conditions is greater than 99%.
- Reactor 22 is an eight-stage upflow reactor in which dehydrohalogenation of 3,4-dichlorobutene-1 to 2-chloro-1,3-butadiene (i.e. chloroprene) takes place.
- the reactor contains 8 perforated metal plates, 26 , 28 , 30 , 32 , 34 , 36 , 38 , and 40 .
- Water, 50% sodium hydroxide, phase transfer catalyst, and liquid dichlorobutene reactant are fed through lines 10 , 12 , 14 , and 16 , respectively, to line 18 to form a two-phase aqueous/organic liquid stream.
- streams 10 and 12 could alternatively be mixed and fed to reactor 8 independently of streams 14 and 16 , or all four streams could be fed independently.
- the stream is fed through line 18 to high shear mixer 42 .
- the high shear mixing causes initiation of the dehydrohalogenation reaction and a rise in temperature.
- the stream is fed through line 20 to reactor 22 .
- Dehydrohalogenation of the dichlorobutene continues causing formation of water, chloroprene and sodium chloride.
- the chloroprene is vaporized along with a portion of the water and is conducted, along with catalyst, sodium hydroxide, sodium chloride and water, up and out through the top of the column.
- the stream may then be fed via line 44 to steam strippers where chloroprene is removed and by-products are recovered for recycle or disposal.
- vapor that exits the column overhead consisting predominantly of chloroprene and water, can be fed to a condenser.
- the liquid that exists the column overhead consisting of an organic and aqueous phase, can be conducted to a stripper or other distillation device.
- An organic liquid composed of 99.5 wt. % 3,4-dichlorobutene-1, and 0.17 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst was fed at a rate of 87 kg/hour to a 0.014 cubic meter metal mixing vessel fitted with a mechanical paddle wheel agitator.
- An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water was also fed to the same mixing vessel at a rate of 142 kg/hour.
- the reactant stream from the mixing vessel was fed continuously to the bottom of a vertical 21 cm diameter, 7.3 m tall metal upflow reactor column having 14 stages.
- An organic liquid composed of 99.5 wt. % 2,3,4-trichlorobutene-1 and 0.13 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of 109 kg/hr to a 0.021 cubic meter metal mixing vessel fitted with a mechanical paddle wheel agitator.
- An aqueous stream composed of 21.7 wt. % sodium hydroxide, 77.5 wt. % water, and 0.8 wt. % sodium chloride is also fed to the same mixing vessel at 179.5 kg/hr.
- the mixed stream from the mixing vessel is fed continuously to the bottom of of a vertical 21 cm diameter, 4.9 m tall, metal upflow reactor column having eight stages.
- Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid.
- the vaporized dehydrochlorinated product of the reaction i.e. 2,3-dichlorobutadiene-1,3, and water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases.
- the reaction heat maintains the temperature at the bottom of the column at approximately 70° C. and the temperature at the top of the column is approximately 50° C.
- the pressure at the bottom of the column is approximately 0.06 MPa and the pressure at the top is maintained at approximately 0.025 MPa.
- liquid is vaporized continuously as volatile product forms and pressure continuously drops.
- the vapor and liquid from the top of the column are fed to a condenser and cooled to 25° C.
- the organic liquid phase from the condenser is 2,3-dichlorobutadiene-1,3, which forms in yields in excess of 99%.
- An organic liquid composed of 99.5 wt. % perfluorobutylethyl iodide and 0.2 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of approximately 340 kg/hr to a 0.021 cubic meter mixing vessel fitted with a mechanical paddle wheel agitator.
- An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water is fed to the same mixing vessel at approximately 198 kg/hr.
- the mixed stream from the mixing vessel is fed continuously to the bottom of a vertical 21 cm diameter, 6.1 m tall, metal upflow reactor column having ten stages.
- Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid.
- the vaporized dehydroiodinated product of the reaction i.e perfluorobutylethylene
- water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases.
- the reaction heat maintains the temperature at the bottom of the column at approximately 75° C. and the temperature at the top of the column at approximately 60° C.
- the pressure at the top of the column is maintained at ambient pressure.
- liquid is vaporized continuously as volatile product forms and pressure continuously drops.
- the vapor and liquid from the top of the column are fed to a condenser and cooled to approximately 25° C.
- the organic liquid phase from the condenser is perfluorobutylethylene, which forms in excess of 95%.
- An organic liquid composed of 99.5 wt. % 1,4-dibromo-1,1,2,2-tetrafluorobutane and 0.2 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of approximately 262 kg/hr to a mixing vessel fitted with a mechanical paddle wheel agitator.
- An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water is fed to the same mixing vessel at approximately 200 kg/hr.
- the mixed stream from the mixing vessel is fed continuously to the bottom of of a vertical 21 cm diameter, 6.1 m tall, metal upflow reactor column having ten stages.
- Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid.
- the vaporized dehydrobrominated product of the reaction i.e 4-bromo-3,3,4,4-tetrafluorobutene
- water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases.
- the reaction heat maintains the temperature at the bottom of the column at approximately 75° C. and the temperature at the top of the column approximately 57° C.
- the pressure at the top of the column is maintained at ambient pressure.
- liquid is vaporized continuously as volatile product forms and pressure continuously drops.
- the vapor and liquid from the top of the column are fed to a condenser and cooled to approximately 25° C.
- the organic liquid phase from the condenser is 4-bromo-1,1,2,2-tetrafluorobutene.
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Abstract
Description
- This application claims the benefit of U.S. Provisional Application No. 60/225,920 filed Aug. 17, 2000.
- This invention relates to an improved process for production of alkenes from halogenated organic compounds. More specifically, this invention relates to a process for dehydrohalogenation of halogenated organic compounds using a staged upflow reactor.
- Dehydrohalogenation of halogenated organic compounds is generally conducted in the liquid phase by mixing a halogenated alkane or halogenated alkene with a strong base in a solvent. Because the base is usually added as an aqueous solution, phase transfer catalysts are often employed to promote contact of the reactants.
- In many processes a series of continuous stirred tank reactors are used and by-products of the reaction, as well as unreacted starting materials, are removed by steam stripping or distillation. For example, 2-chloro-1,3-butadiene can be prepared by dehydrohalogenation of 3,4-dichlorobutene-1 in a series of co-current continuous stirred tank reactors using the catalytic process disclosed in U.S. Pat. No. 3,981,937. Other processes involve the use of boiling reactors, for example as disclosed in U.S. Pat. No. 3,772,461, or in stirred tanks coupled with phase decantation as disclosed in U.S. Pat. No. 4,418,232. Each of these methods is associated with disadvantages. The stirred reactor processes suffer from relatively low conversions and result in production of high levels of organic waste. Conversions in one-pass boiling reactor processes are typically extremely low, for example 85% or less. In addition, investment and energy costs associated with such processes are high.
- Dehydrohalogenation processes that result in improved reactant conversion levels would result in production of lower levels of organic waste. These more efficient processes reduce production of halogenated organic compounds that can contribute to global warming. In addition, energy and material consumption are reduced.
- The present invention is directed to an improved process for dehydrohalogenation of organic compounds. In particular, the present invention relates to a process for dehydrohalogenation of a halogenated compound selected from the group consisting of halogenated alkanes and halogenated alkenes, said process comprising
- A) contacting a first composition comprising said halogenated compound with a second composition comprising a base having a Kb of at least 10−9, in the liquid phase, in a reactor having multiple stages, at a temperature sufficient to initiate the exothermic reaction of said halogenated compound with said base, thereby forming a dehydrohalogenated compound having a boiling point lower than that of said halogenated compound; and
- B) maintaining the temperature of the reactor contents at a temperature sufficient to vaporize said dehydrohalogenated compound thereby causing agitation of said reactor contents and transfer of vaporized dehydrohalogenated compound through said multiple stages of said reactor, said vaporization providing a means of agitation.
- FIG. 1 is a schematic diagram of one embodiment of the process of the present invention.
- The dehydrohalogenation process of the present invention takes place in the liquid phase in a staged bubble reactor. Bubble reactors are extensively used in the chemical industry and consist of a contact region in which a discontinuous gas phase in the form of bubbles moves relative to a continuous phase. Bubble reactors can be single staged or multistaged, single channel or multi-channel, batch or continuous. A preferred type of bubble reactor is a co-current vertical column containing multiple stages, hereinafter referred to as a multi-staged upflow reactor.
- The halogenated organic compound or compounds that serve as the reactants may be selected from the group consisting of halogenated aliphatic alkanes or halogenated aliphatic alkenes. Preferred compounds are those having two to eight carbon atoms. Any saturated or unsaturated halogenated alkane or halogenated alkene that can be dehydrohalogenated with alkali is suitable for use in the process of the invention. These halogenated compounds will have at least one hydrogen atom. Fluorinated, chlorinated, brominated or iodinated alkanes or alkenes are all suitable reactants. Preferred halogenated compound reactants are chlorinated butadienes or chlorinated butenes. The halogenated alkanes or alkenes may contain a single species of halogen atom or they may contain more than one type of halogen atom. The process is particularly useful for dehydrochlorination of chlorinated alkanes and chlorinated alkenes in the presence of aqueous alkali. Examples of suitable halogenated alkanes or halogenated alkenes include 1,4-dichlorobutene-2; 3,4-dichlorobutene-1; 2,3,4-trichlorobutene-1; 2-chloro-3-bromobutene-1; 1,2-dibromopropane; 1,3-dichlorobutane; 1-iodo-2-chlorobutane; perfluorobutylethyliodide; and 1,4-dibromo-1,1,2,2-tetrafluorobutane.
- The halogenated reactant may be in the form of a solid, a liquid or a gas at ambient temperature. However, liquid halogenated alkanes or alkenes are preferred. In addition, the halogenated reactant must either be a liquid or be present in a liquid phase under the conditions at which the dehydrohalogenation reaction is conducted.
- The dehydrohalogenating agent, which is a base having a Kb of at least 10−9, will generally be in the form of an aqueous solution, but it need not be. Suitable bases include pyridine, trimethylamine, ammonia, ammonium hydroxide, calcium hydroxide, alkali metal hydroxides, and alkali metal alkoxides. Preferably the base will have a Kb of at least 10−5, and most preferably the base will be completely ionized, as in the case of aqueous alkali. Any aqueous alkali metal hydroxide is suitable for purposes of the invention, but sodium hydroxide and potassium hydroxide are preferred. The alkali normally will be present in excess in the reaction mixture. Generally, a mole ratio of alkali to halogenated reactant will be approximately 1.01-2.00. The precise amount will be determined based on factors such as the type of catalyst used and the particular reactants.
- The reaction takes place in the liquid phase. The reaction mixture will normally contain at least one liquid. For example, the halogenated reactants may be liquids under conditions of the reaction or they may be dissolved in aqueous or non-aqueous solvents. If the reactants are present as solutions, the solvents may be miscible or immiscible. In a preferred embodiment the halogenated reactant is a liquid and an alkali metal hydroxide dehydrohalogenating agent is present as an aqueous solution. In addition, the dehydrohalogenation may take place in the presence of a non-aqueous solvent such as methanol, for example as disclosed in U.S. Pat. No. 4,104,316.
- Preferably, especially in those cases where a halogenated liquid reactant is reacted with an aqueous solution of alkali metal hydroxide, a phase transfer catalyst is used to promote contact between the two immiscible liquids, i.e. the organic and aqueous phases. Preferred catalysts are quaternary ammonium salts, especially quaternary ammonium chlorides, particularly those represented by the formula R1R2R3R4NCl in which each of R1, R2 and R3 independently is a C1-C20 alkyl, a C2-C20 alkenyl, or a C7-C20 aralkyl, and R4 is a C6-C20 alkyl or alkenyl, benzyl, or a (C6-C20) alkyl- or alkenyl-substituted benzyl. Each of R1, R2, and R3 groups in these quaternary ammonium chlorides may also contain a hydroxyl or ether group in a position beta to the nitrogen atom. The amount of the quaternary ammonium compound is generally about 0.01-10% by weight of the starting halogenated alkane or alkene. Other phase transfer catalysts include amine oxides, such as those disclosed in U.S. Pat. No. 3,876,716 and quaternary phosphonium compounds, such as those disclosed in U.S. Pat. No. 3,639,493.
- Other optional components may be present in the reaction mixture, for example inhibitors, stabilizers and dispersants. The use of such optional components will depend on the nature of the reactants and products to be produced.
- In the process of the present invention, the halogenated alkane or halogenated alkene, and the base, are contacted in a bubble reactor in a liquid phase, thereby initiating an exothermic reaction to produce a dehydrohalogenated compound having a boiling point lower than that of the halogenated reactant. The heat liberated during the reaction vaporizes the dehydrohalogenated compound thus produced. It is to be understood that, if the halogenated alkane or alkene contains more than one site at which dehydrohalogenation can occur, then simultaneous dehydrohalogenation may take place. Thus, for example a halogenated alkane such as 1-chloro-4-bromobutane will lose hydrogen bromide and some hydrogen chloride when subjected to the conditions of the process of the present invention.
- The vaporized product and water vapor that forms as a result of the dehydrohalogenation constitutes the gaseous phase that provides agitation of the reaction mixture as it moves through the reactor. Consequently, no internal stirring device is necessary within the reactor. Optionally, stirring means, such as a mechanical stirrer, can be present, but the presence of such devices is not necessary. Because the reaction is exothermic, it is not necessary to supply external heat to the reactor. In some instances it is useful to supply a small amount of heat initially for purposes of initiating the reaction or for temperature control.
- The reactor is a multi-stage type, preferably having at least three stages, most preferably 4-20 stages. Reactors having only one stage provide low single pass conversion. Consequently, separation and recycle of the unconverted reactants must be undertaken which increases complexity and cost of the process when used on an industrial scale. Preferably the reactor will be a vertical column reactor because it greatly simplifies flow from stage to stage. That is, when an upflow reactor is employed, liquid reactants are entrained up through the stages by the rising bubbles. This eliminates the need for pumps to transfer reactants from stage to stage. In addition, the process of the present invention can take place in a series of continuous, distinct tanks or vessels.
- In a preferred embodiment, chlorinated alkane or chlorinated alkene reactant and aqueous alkali metal hydroxide will be pre-mixed before introduction to the reactor. Examples of mixing devices include tanks fitted with mechanical agitators, that is stirred tank reactors, continuous stirred tank reactors, pumps and motionless stationary mixers. Reaction is initiated in the mixing device. This exothermic reaction provides heat and raises the vapor pressure to the point where some evaporation occurs upon entry to the bubble reactor. Mixing devices that are particularly useful in the practice of the invention include homogenizers, colloid mills, stirred tank reactors and centrifugal pumps.
- Prior art bubble reactor processes typically involve introduction of a single gas phase and a single liquid phase to the reactor. Other variations include the combination of a gas phase plus a solid phase or a three phase process involving a liquid, gas and a solid phase, i.e. a slurry. Such processes are discussed by Y. T. Shah, et al. inDesign Parameters Estimations for Bubble Column Reactors, American Institute of Chemical Engineers Journal, 28, No. 3, 353 (1982) and S. Lee and Y. Tsui, Succeed at Gas/Liquid Contacting, Chemical Engineering Progress, 23 (July 1999). In the present process two liquids, but no gases, are fed to the system. The gas, which is necessary for functioning of the bubble reactor, is generated in situ by the present process. This provides an agitation means for the bubble reactor, preferably the primary means of agitation, thereby decreasing the complexity of the process and increasing overall efficiency. Mass transfer from the gas to the liquid is not a factor that influences the reaction. The gas is a working fluid that controls temperature by its formation and provides agitation by virtue of its buoyancy. Further, the gas formation greatly enhances the kinetic efficiency of the reaction.
- The process of the present invention is useful for production of a wide variety of dehydrohalogenated products, for example, 2-methyl-3-chloropropene-1; 2-bromopropene-1; 3-chlorobutene-2; 2,3-dichloro-1-3-butadiene; perfluorobutylethylene; and 4-bromo-3,3,4,4-tetrafluorobutene. It is particularly useful in production of chloroprene from 3,4-dichlorobutene-2.
- The process of the present invention enhances the kinetics of the dehydrohalogenation process. That is, it promotes concentration of the catalyst and reactants, due to evaporation of the product, thus resulting in an increase in reaction rate. The process is most effective when the boiling point of the base used is between that of the dehydrohalogenated product and the organic reactant. In instances where an aqueous base is utilized, the boiling point of the base will be that of the aqueous base solution, under the particular reaction conditions. For example, 3,4-dichlorobutene-1 can be dehydrohalogenated to form chloroprene in the presence of 22 wt. % aqueous sodium hydroxide according to the present invention. The boiling point of water in a 22 wt. % aqueous sodium hydroxide solution is 110°-111° C. Under the temperature and pressure conditions of the reaction, the boiling points of chloroprene and 3,4-dichlorobutene-1 are 59° C. and 126° C., respectively. The yield of product under these conditions is greater than 99%.
- Reference is now made to FIG. 1 which illustrates a preferred embodiment of the process of the present invention.
Reactor 22 is an eight-stage upflow reactor in which dehydrohalogenation of 3,4-dichlorobutene-1 to 2-chloro-1,3-butadiene (i.e. chloroprene) takes place. The reactor contains 8 perforated metal plates, 26, 28, 30, 32, 34, 36, 38, and 40. Water, 50% sodium hydroxide, phase transfer catalyst, and liquid dichlorobutene reactant are fed throughlines streams line 18 tohigh shear mixer 42. The high shear mixing causes initiation of the dehydrohalogenation reaction and a rise in temperature. After passing throughmixer 42, the stream is fed throughline 20 toreactor 22. Dehydrohalogenation of the dichlorobutene continues causing formation of water, chloroprene and sodium chloride. The chloroprene is vaporized along with a portion of the water and is conducted, along with catalyst, sodium hydroxide, sodium chloride and water, up and out through the top of the column. The stream may then be fed vialine 44 to steam strippers where chloroprene is removed and by-products are recovered for recycle or disposal. Alternatively, vapor that exits the column overhead, consisting predominantly of chloroprene and water, can be fed to a condenser. The liquid that exists the column overhead, consisting of an organic and aqueous phase, can be conducted to a stripper or other distillation device. - The invention is further illustrated in the embodiments below wherein all parts are by weight.
- An organic liquid composed of 99.5 wt. % 3,4-dichlorobutene-1, and 0.17 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst was fed at a rate of 87 kg/hour to a 0.014 cubic meter metal mixing vessel fitted with a mechanical paddle wheel agitator. An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water was also fed to the same mixing vessel at a rate of 142 kg/hour. The reactant stream from the mixing vessel was fed continuously to the bottom of a vertical 21 cm diameter, 7.3 m tall metal upflow reactor column having 14 stages. Each stage was separated with perforated metal plates designed to minimize back-flow of liquid. The vaporized dehydrochlorinated product of the reaction, i.e. 2-chloro-1,3-butadiene, and water vapor rose through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases. The heat of reaction maintained the temperature at the bottom of the column at 80° C. and the temperature at the top of the column was 66° C. The pressure at the bottom of the column was 0.17 MPa and the pressure at the top was 0.12 MPa. As the two liquid phases flowed up through the column, liquid vaporized continuously as volatile product formed and pressure continuously dropped. The liquid stream leaving the top of the column was composed of 3 wt. % organic phase and 97 wt. % aqueous phase. Catalyst concentration in the liquid stream leaving the column was 2.9 wt. %. The overhead vapor from the column contained 95 wt. % of organic product and 5 wt. % water vapor. The overhead vapor and liquid streams were fed to a condenser and cooled to 20° C. Analysis of the organic liquid phase from the condenser indicated conversion of the 3,4-dichlorobutene-1 to 2-chloro-1,3 butadiene was 99.7%.
- An organic liquid composed of 99.5 wt. % 2,3,4-trichlorobutene-1 and 0.13 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of 109 kg/hr to a 0.021 cubic meter metal mixing vessel fitted with a mechanical paddle wheel agitator. An aqueous stream composed of 21.7 wt. % sodium hydroxide, 77.5 wt. % water, and 0.8 wt. % sodium chloride is also fed to the same mixing vessel at 179.5 kg/hr. The mixed stream from the mixing vessel is fed continuously to the bottom of of a vertical 21 cm diameter, 4.9 m tall, metal upflow reactor column having eight stages. Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid. The vaporized dehydrochlorinated product of the reaction, i.e. 2,3-dichlorobutadiene-1,3, and water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases. The reaction heat maintains the temperature at the bottom of the column at approximately 70° C. and the temperature at the top of the column is approximately 50° C. The pressure at the bottom of the column is approximately 0.06 MPa and the pressure at the top is maintained at approximately 0.025 MPa. As the two liquid phases flow up through the column, liquid is vaporized continuously as volatile product forms and pressure continuously drops. The vapor and liquid from the top of the column are fed to a condenser and cooled to 25° C. The organic liquid phase from the condenser is 2,3-dichlorobutadiene-1,3, which forms in yields in excess of 99%.
- An organic liquid composed of 99.5 wt. % perfluorobutylethyl iodide and 0.2 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of approximately 340 kg/hr to a 0.021 cubic meter mixing vessel fitted with a mechanical paddle wheel agitator. An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water is fed to the same mixing vessel at approximately 198 kg/hr. The mixed stream from the mixing vessel is fed continuously to the bottom of a vertical 21 cm diameter, 6.1 m tall, metal upflow reactor column having ten stages. Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid. The vaporized dehydroiodinated product of the reaction, i.e perfluorobutylethylene, and water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases. The reaction heat maintains the temperature at the bottom of the column at approximately 75° C. and the temperature at the top of the column at approximately 60° C. The pressure at the top of the column is maintained at ambient pressure. As the two liquid phases flow up through the column, liquid is vaporized continuously as volatile product forms and pressure continuously drops. The vapor and liquid from the top of the column are fed to a condenser and cooled to approximately 25° C. The organic liquid phase from the condenser is perfluorobutylethylene, which forms in excess of 95%.
- An organic liquid composed of 99.5 wt. % 1,4-dibromo-1,1,2,2-tetrafluorobutane and 0.2 wt. % bis (beta hydroxypropyl)cocobenzylamine chloride salt catalyst is fed at a rate of approximately 262 kg/hr to a mixing vessel fitted with a mechanical paddle wheel agitator. An aqueous stream composed of 22 wt. % sodium hydroxide and 78 wt. % water is fed to the same mixing vessel at approximately 200 kg/hr. The mixed stream from the mixing vessel is fed continuously to the bottom of of a vertical 21 cm diameter, 6.1 m tall, metal upflow reactor column having ten stages. Each stage is separated with a perforated metal plate designed to minimize back-flow of liquid. The vaporized dehydrobrominated product of the reaction, i.e 4-bromo-3,3,4,4-tetrafluorobutene, and water vapor rises through the column causing agitation and upward entrainment of the immiscible liquid organic and aqueous phases. The reaction heat maintains the temperature at the bottom of the column at approximately 75° C. and the temperature at the top of the column approximately 57° C. The pressure at the top of the column is maintained at ambient pressure. As the two liquid phases flow up through the column, liquid is vaporized continuously as volatile product forms and pressure continuously drops. The vapor and liquid from the top of the column are fed to a condenser and cooled to approximately 25° C. The organic liquid phase from the condenser is 4-bromo-1,1,2,2-tetrafluorobutene.
Claims (17)
Priority Applications (8)
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JP2002519396A JP4896352B2 (en) | 2000-08-17 | 2001-08-17 | Method for dehydrohalogenation of halogenated compounds |
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DE60121772T DE60121772T2 (en) | 2000-08-17 | 2001-08-17 | METHOD FOR DEHYDROHALOGENATING HALOGENATED COMPOUNDS |
CN01141116A CN1344702A (en) | 2000-08-17 | 2001-08-17 | Method for elimination of hydrogen halides for halogenated compound |
EP01962242A EP1309530B1 (en) | 2000-08-17 | 2001-08-17 | Process for dehydrohalogenation of halogenated compounds |
CNB018142370A CN1262526C (en) | 2000-08-17 | 2001-08-17 | Process for dehydrohalogenation of halogenated compounds |
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- 2001-08-17 DE DE60121772T patent/DE60121772T2/en not_active Expired - Lifetime
- 2001-08-17 JP JP2002519396A patent/JP4896352B2/en not_active Expired - Fee Related
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- 2001-08-17 CN CNB018142370A patent/CN1262526C/en not_active Expired - Lifetime
- 2001-08-17 EP EP01962242A patent/EP1309530B1/en not_active Expired - Lifetime
- 2001-08-17 WO PCT/US2001/025816 patent/WO2002014247A2/en active IP Right Grant
- 2001-08-17 JP JP2001247583A patent/JP2002087997A/en not_active Withdrawn
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Publication number | Publication date |
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WO2002014247A2 (en) | 2002-02-21 |
EP1309530B1 (en) | 2006-07-26 |
EP1309530A2 (en) | 2003-05-14 |
CN1447782A (en) | 2003-10-08 |
JP2004506031A (en) | 2004-02-26 |
WO2002014247A3 (en) | 2002-08-29 |
CN1344702A (en) | 2002-04-17 |
US6380446B1 (en) | 2002-04-30 |
CN1262526C (en) | 2006-07-05 |
DE60121772D1 (en) | 2006-09-07 |
JP2002087997A (en) | 2002-03-27 |
DE60121772T2 (en) | 2007-08-02 |
JP4896352B2 (en) | 2012-03-14 |
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