WO2014164001A1 - Method to reduce the formation of high boiling compounds during the dehydrochlorination of 1,1,1,3- tetrachloropropane - Google Patents

Method to reduce the formation of high boiling compounds during the dehydrochlorination of 1,1,1,3- tetrachloropropane Download PDF

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Publication number
WO2014164001A1
WO2014164001A1 PCT/US2014/019794 US2014019794W WO2014164001A1 WO 2014164001 A1 WO2014164001 A1 WO 2014164001A1 US 2014019794 W US2014019794 W US 2014019794W WO 2014164001 A1 WO2014164001 A1 WO 2014164001A1
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WO
WIPO (PCT)
Prior art keywords
hcc
trichloropropene
dehydrochlorination
tetrachloropentane
isomers
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/US2014/019794
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English (en)
French (fr)
Inventor
Terris YANG
Joshua Close
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
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Honeywell International 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 Honeywell International Inc filed Critical Honeywell International Inc
Priority to EP14778850.9A priority Critical patent/EP2970064A4/en
Priority to CN201480014679.8A priority patent/CN105121394B/zh
Priority to JP2016500539A priority patent/JP2016510814A/ja
Priority to MX2015012041A priority patent/MX2015012041A/es
Publication of WO2014164001A1 publication Critical patent/WO2014164001A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/26—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton
    • C07C17/272—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions
    • C07C17/275—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions of hydrocarbons and halogenated hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C19/00—Acyclic saturated compounds containing halogen atoms
    • C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C21/00—Acyclic unsaturated compounds containing halogen atoms
    • C07C21/02—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds
    • C07C21/04—Chloro-alkenes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/26—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton
    • C07C17/263—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by condensation reactions
    • C07C17/269—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by condensation reactions of only halogenated hydrocarbons

Definitions

  • the compound 1,1,3-trichloropropene is useful as a chemical intermediate in the formation of other commercially important compounds. See, for example, U.S. Patent Pub. No. 2012-0142980, the disclosure of which is hereby incorporated herein by reference.
  • This invention relates to a method to improve the selectivity to 1,1,3-trichloropropene and/or 3,3,3-trichloropropene by the catalytic dehydrochlorination of HCC- 250fb, 1,1,1,3-tetrachloropropane.
  • FeCl 3 is used as the catalyst for the dehydrochlorination of HCC-250fb to produce 1,1,3-trichloropropene and/or 3,3,3- trichloropropene. See, for example, US Patent Pub. No. 2012-0035402, the disclosure of which is hereby incorporated herein by reference.
  • HBCs high boiling compounds
  • pentachlorocyclohexene and/or hexachlorocyclohexane species in addition to the desired product, namely 1,1,3- trichloropropene and/or 3,3,3-trichloropropene.
  • the formation of these HBCs is due to the dimerization of the reaction products, which can include the propene isomers, 1,1,3-trichloropropene and/or 3,3,3-trichloropropene.
  • the formation of these HBCs reduces the selectivity to the desired product, 1,1,3-trichloro-propene and/or 3,3,3-trichloropropene.
  • HCC-250fb is produced from CC1 4 and ethylene with catalysts under certain reaction conditions.
  • the catalysts used in the reaction are removed from the crude HCC-250fb product by distillation (Catalyst Recycle Column or CRC).
  • CRC Catalyst Recycle Column
  • the "top” stream from CRC is fed to a lights distillation column to remove unreacted CC1 4 and ethylene.
  • the "bottom” stream (namely HCC-250fb + Heavies) of the lights column is then fed into a third distillation column with pure HCC-250fb collected from the "top” stream.
  • the pure HCC-250fb is then used as the raw material in a dehydrochlorination process to make 1,1,3-trichloropropene and/or 3,3,3-trichloropropene (hereafter the "step 2" process).
  • the present invention is based upon the discovery that the crude "bottom" stream from the step 1 process, which comprises a mixture of HCC-250fb and "Heavies" from the lights distillation column in the step 1 process, can be used as the raw material for the dehydrochlorination process to make 1,1,3-trichloropropene and/or 3,3,3-trichloropropene; and when this crude starting material was used, the formation of HBCs was significantly suppressed or eliminated.
  • tetrachloropentane isomers such as 1,1,1,5- and 1,3,3,5-tetrachloropentane
  • 1,1,1,5- and 1,3,3,5-tetrachloropentane are present in the crude mixture of HCC-250fb + Heavies. These compounds are believed to play a role regarding both HCC-250fb conversion and HBC selectivity.
  • certain trichloropentene isomers are produced by the dehydrochlorination of these tetra- chloropentane isomers. These compounds can also inhibit the formation of HBCs. See the data shown in Figs. 1 and 2.
  • one embodiment of the present invention is directed to a process for the dehydrochlorination of HCC-250fb to produce 1,1,3-trichloropropene and/or 3,3,3- trichloropropene using as the starting material, a crude mixture of HCC-250fb + Heavies generated from the step 1 process.
  • certain of the Heavies included in this composition comprise tetrachloropentane isomers, such as 1,1,1,5- tetrachloro- pentane and/or 1,3,3,5-tetrachloropentane.
  • another embodiment of the present invention is directed to a process for the dehydrochlorination of HCC-250fb to produce 1,1,3-trichloropropene and/or 3,3,3-trichloropropene using as the starting material, a mixture of HCC-250fb and one or more tetrachloropentane isomers, such as 1,1,1,5- and 1,3,3,5-tetrachloropentane.
  • one embodiment of the present invention is directed to a process for the dehydrochlorination of HCC-250fb to produce 1,1,3-trichloropropene and/or 3,3,3-trichloropropene using as the starting material, a mixture of HCC-250fb and one or more trichloropentene isomers.
  • one embodiment of the present invention is directed to a process for the dehydrochlorination of HCC-250fb + Heavies to produce 1,1,3-trichloropropene and/or 3,3,3-trichloropropene using one or more metal halides or mixtures, such as FeCl 3 and/or FeCl 2 , as the catalyst.
  • metal halides or mixtures such as FeCl 3 and/or FeCl 2
  • Figure 1 shows the effect of trichloropentene isomers on HCC-250fb conversion in HCC-250 dehydrochlorination.
  • Figure 2 shows the effect of trichloropentene isomers on HBC selectivity in HCC- 250 dehydrochlorination.
  • the HCC-250 dehydrochlorination process can be conducted with significant reduction or elimination of unwanted HBCs, together with significantly improvement in the selectivity to the target products (1,1,3- trichloropropene and/or 3,3,3-trichloropropene).
  • This improved selectivity is beneficial to the reduction of process waste and it simplifies the future separation of crude product for the combined step 1 and step 2 process reactions, and therefore reduces the overall production costs.
  • the catalytic HCC-250fb dehydrochlorination reaction is preferably carried out under conditions to attain a starting material conversion of at least about 20% or higher, preferably at least about 40% or higher, and even more preferably at least about 60% or higher, and a desired product 1,1, 3 -trichloropropene and/or 3,3,3-trichloropropene selectivity of at least about 50% or higher, preferably at least about 70% or higher, and more preferably at least about 95% or higher. Selectivity is calculated by the number of moles of product formed divided by the number of moles of reactant consumed.
  • Useful reaction temperatures for the catalytic dehydrochlorination reaction may range from about 50°C to about 300°C. Preferred temperatures may range from about 70°C to about 150°C, and more preferred temperatures may range from about 100°C to about 125°C. One especially preferred reaction temperature is about 120°C.
  • the reaction may be conducted at atmospheric pressure, super-atmospheric pressure or under vacuum. The vacuum pressure can be from about 0 torr to about 760 torr.
  • Contact time of the reactant starting materials with the catalyst mixture may range from about 0.5 to 10 hours, preferably from about 2 to 8 hours, more preferably about 4 hours, however, longer or shorter times can be used.
  • the reactor was stirred and heated to 120° ⁇ 2°C via an oil bath. After 4 hours, the reactor was removed from the oil bath and cooled down to room temperature. Then the mixture in the reactor was filtered, washed with D.I. water and dried with MgSC .
  • the reaction mixture contained 73.3 wt% of 1,1,3 -trichloropropene, 1.9 wt% of HCC-250f and 24.6 wt% of HBCs, representing a HCC-250f conversion of 98.3 mol%, 1,1, 3 -trichloropropene selectivity of 84.2 mol%, and HBCs selectivity of 15.8 mol%.
  • Example 2 The same apparatus as described in Example 1 was charged with 100.4 g HCC- 250fb + Heavies (Honeywell, 98.0 wt%) and 0.107 g FeCl 3 .
  • the reaction mixture contained 51.4 wt% of 1,1,3-trichloropropene, 45.8 wt% of HCC-250fb and 1.0 wt% of HBCs, representing a HCC-250fb conversion of 58.6 mol%, 1,1,3- trichloropropene selectivity of 99.0 mol% and HBCs selectivity of 1.0 mol%.
  • Example 2 The same apparatus as described in Example 1 was charged with 100.0 g HCC- 250fb + Heavies (Honeywell, 98.0 wt%) and 0.101 g FeCl 3 .
  • the reaction mixture contained 52.1 wt% of 1,1,3-trichloropropene, 44.6 wt% of HCC-250fb and 1.9 wt% of HBCs, representing a HCC-250fb conversion of 59.6 mol%, 1,1,3-trichloropropene selectivity of 98.1 mol% and HBCs selectivity of 1.9 mol%.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
PCT/US2014/019794 2013-03-12 2014-03-03 Method to reduce the formation of high boiling compounds during the dehydrochlorination of 1,1,1,3- tetrachloropropane Ceased WO2014164001A1 (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP14778850.9A EP2970064A4 (en) 2013-03-12 2014-03-03 METHOD FOR REDUCING THE FORMATION OF HIGH-END CONNECTIONS DURING THE DEHYDROCHLORATION OF 1,1,1,3-TETRACHLOROPROPANE
CN201480014679.8A CN105121394B (zh) 2013-03-12 2014-03-03 减少1，1，1，3‑四氯丙烷脱氯化氢期间高沸点化合物形成的方法
JP2016500539A JP2016510814A (ja) 2013-03-12 2014-03-03 １，１，１，３−テトラクロロプロパンの脱塩酸反応において高沸点化合物の生成を低減する方法
MX2015012041A MX2015012041A (es) 2013-03-12 2014-03-03 Metodo para reducir la formacion de compuestos de alto punto de ebullicion durante la deshidrocloracion de 1,1,1,3-tetracloropropa no.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US13/796,328 US8889927B2 (en) 2013-03-12 2013-03-12 Method to reduce the formation of high boiling compounds during the dehydrochlorination of 1,1,1,3-tetrachloropropane
US13/796,328 2013-03-12

Publications (1)

Publication Number Publication Date
WO2014164001A1 true WO2014164001A1 (en) 2014-10-09

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Country Status (6)

Country Link
US (1) US8889927B2 (enExample)
EP (1) EP2970064A4 (enExample)
JP (1) JP2016510814A (enExample)
CN (2) CN107266286B (enExample)
MX (1) MX2015012041A (enExample)
WO (1) WO2014164001A1 (enExample)

Cited By (1)

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JP2021006541A (ja) * 2014-10-16 2021-01-21 スポレク プロ ヘミコウ アー フツニ ブイロブ，アクツィオバ スポレチェノスト 方法

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CZ309260B6 (cs) 2014-10-16 2022-06-29 Spolek Pro Chemickou A Hutní Výrobu, Akciová Společnost Způsob přípravy chlorovaného alkenu
WO2017223338A1 (en) * 2016-06-23 2017-12-28 Blue Cube Ip Llc Process for the dehydrochlorination of a chloroalkane
CN109809959B (zh) 2017-11-22 2021-10-01 江西天宇化工有限公司 一种1,1,1,2,3-五氯丙烷的制备方法
WO2019195250A1 (en) 2018-04-03 2019-10-10 Blue Cube Ip Llc Method for the production of a halogenated alkene by catalyzed dehydrohalogenation of a halogenated alkane
WO2020041731A1 (en) 2018-08-24 2020-02-27 Blue Cube Ip Llc Gallium catalyzed dehydrochlorination of a chlorinated alkane
CN111643917B (zh) * 2020-06-15 2021-09-17 威海新元化工有限公司 一种1,1,3-三氯丙烯的连续生产装置及方法

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Also Published As

Publication number Publication date
CN105121394A (zh) 2015-12-02
EP2970064A1 (en) 2016-01-20
JP2016510814A (ja) 2016-04-11
CN105121394B (zh) 2017-06-20
MX2015012041A (es) 2015-12-16
CN107266286B (zh) 2020-09-04
US20140275658A1 (en) 2014-09-18
EP2970064A4 (en) 2016-09-21
CN107266286A (zh) 2017-10-20
US8889927B2 (en) 2014-11-18

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