EP0662938A1 - Process for converting 1,1,1,2-tetrachloroethane to vinylidene chloride - Google Patents
Process for converting 1,1,1,2-tetrachloroethane to vinylidene chlorideInfo
- Publication number
- EP0662938A1 EP0662938A1 EP93920024A EP93920024A EP0662938A1 EP 0662938 A1 EP0662938 A1 EP 0662938A1 EP 93920024 A EP93920024 A EP 93920024A EP 93920024 A EP93920024 A EP 93920024A EP 0662938 A1 EP0662938 A1 EP 0662938A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- percent
- elemental
- group
- catalyst
- tetrachloroethane
- 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
Links
Classifications
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- 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
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
- B01J23/52—Gold
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8926—Copper and noble metals
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8966—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with germanium, tin or lead
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/26—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/26—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms
- C07C1/30—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms by splitting-off the elements of hydrogen halide from a single molecule
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/23—Preparation of halogenated hydrocarbons by dehalogenation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/18—Carbon
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of germanium, tin or lead
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/18—Arsenic, antimony or bismuth
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/42—Platinum
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/44—Palladium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/46—Ruthenium, rhodium, osmium or iridium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/48—Silver or gold
- C07C2523/50—Silver
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/48—Silver or gold
- C07C2523/52—Gold
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
- C07C2523/72—Copper
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
- C07C2523/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper combined with noble metals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the material 1,1,1 ,2-tetrachloroethane is produced as a byproduct in the manufacture of 1,2-dichloroethane or EDC, and is a known, useful intermediate for the
- EP 0496- 46A published on July 29, 1992, describes the preparation of chlorotrifluoroethylene and trifluoroethylene from 1, 1,2-trichloro- 1,2,2- -trifiuoroethane via a catalyst comprised of copper and a Group Vlll metal (palladium and platinum being preferred) on a carbon support.
- a catalyst comprised of copper and a Group Vlll metal (palladium and platinum being preferred) on a carbon support.
- EP 015665 describes the conversion of 1,1,2-trichloroethane to ethylene and vinyl ⁇ loride via a catalyst including a noble metal chloride, an alkali metal chloride, iron chloride and optionally copper chloride.
- 1 ,1,1,2-tetrachloroethane is converted to reaction products including vinylidene chloride in a commercially substantial proportion (that is, at a yield (defined as the product of the conversion rate of 1,1,1,2- -tetrachloroethane and the selectivity to vinylidene chloride, on a hydrogen chloride- and hydrogen-free basis) of at least 10 percent, but preferably at least 20 percent, and more
- catalysts including a selected Group IB metal or metals in an elemental or compound form with a selected Group Vlll metal or metals, also in an elemental or compound form.
- Preferred catalysts will, however, consist essentially of a combination of one or more Group IB metals in elemental or compound form with one or more Group Vlll metals in
- the catalysts employed in the processes of the present invention will consist of one or more Group IB metals with one or more Group Vlll metals on a support.
- platinum in elemental or compound form will be employed in these catalysts as a selected Group Vlll metal, with copper in elemental or compound form being
- the Group IB and Group Vlll metals will consist substantially entirely of platinum and copper in their elemental or compound forms, and a most preferred catalyst will employ only platinum and copper in their elemental or compound forms as the Group IB and Group Vlll metals.
- a selected Group IB metal can be from 0.01 to 20 percent by v. eight (on an elemental basis) of these preferred catalysts, with a selected Group Vlll metal (platinum) comprising from 0.01 to 5.0 percent by weight (also on an elemental basis) of the catalyst. More preferably, copper will be from 0.05 to 15 percent by weight of the catalyst (on an elemental basis) and platinum will be from 0.03 to 3.0 percent by weight of the catalyst. Most preferably, the copper can be from 0.1 to 10 percent by weight of the catalyst (on an elemental basis) and platinum will be from 0.05 to 1.0 percent by weight of the catalyst.
- the support can be any of those conventionally employed in the art, but is preferably silica or carbon, and more preferably is carbon. Especially preferred is a high surface area carbon support, for example, a carbon having a specific surface area in an unimpregnated condition of 200 m 2 /g or more, especially 400 m /g or more, and most especially 600 m2/g or more.
- An example of a commercially-available carbon which has been found suitable for use in the present invention is a coal-based carbon produced by Calgon Carbon Corporation under the designation "BPLF3", and may generally be characterized as having a specific surface area of 1100 m /g to 1300 m 2 /g, a pore volume of 0.7 to 0.85 cr ⁇ 3/g, and an average pore radius of 12.3 to 14 angstroms.
- a typical bulk composition of the BPLF3 carbon has been determined to be as follows (by weight percent): silicon, 1.5 percent; aluminum, 1.4 percent; sulfur, 0.75 percent; iron, 0.48 percent; calcium, 0.17 percent; potassium, 0.086 percent; titanium, 0.059 percent; magnesium, 0.051 percent; chlorine, 0.028 percent; phosphorus, 0.026 percent; vanadium, 0.010 percent; nickel, 0.0036 percent; copper, 0.0035 percent; chromium, 0.0028 percent; and manganese, 0.0018 percent (the remainder being carbon).
- Reaction conditions can vary, depending for example on whether the process is to be conducted in the gas phase or in the liquid phase (whether in a batchwise or continuous mode).
- reaction pressures can range from atmospheric pressure up to 1500 psig (10.3 Pa (gauge)), with temperatures of from 100 deg. C. to 350 deg. C, residence times of from 0.25 seconds to 180 seconds, and hydrogen to 1,1,1,2-tetrachloroethane feed ratios ranging on a molar basis from 0.1 : 1 to 100: 1. More preferably, reaction pressures in a gas phase process will range from 5 psig (0.03 Pa (gauge)) to 500 psig (3.4 Pa (gauge)), with temperatures of from 180 deg. C. to 300 deg.
- reaction pressures will range from 40 psig (0.28 Pa (gauge)) to 300 psig (2.1 Pa (gauge)), with temperatures of from 200 deg. C. to 260 deg. C, residence times of from 1 second to 90 seconds, and hydrogen to 1,1,1,2-tetrachloroethane molar feed ratios of from 0.75: 1 to 6: 1.
- reaction pressures are expected to be from atmospheric pressure up to 3000 psig (20.6 Pa (gauge)), at temperatures of from 25 to 350 degrees Celsius, residence times from one to 30 minutes, and hydrogen to 1,1,1,2-tetrachloroethane molar feed ratios of from 0.1 : 1 to 100: 1.
- hydrogen chloride will be included in the feed to the process to reduce coking and catalyst deactivation rates.
- the rate of conversion loss will preferably be no more than about 0.03 percent per hour, and especially no more than about 0.01 percent per hour.
- a catalyst was initially prepared containing 0.5 percent by weight of platinum and 0.9 percent by weight of copper on Calgon's BPLF3 carbon support.
- An aqueous H 2 PtCl6 stock solution was first prepared by dissolving H 2 tCl66H 2 0 (J. T. Baker, Inc.; Baker Analyzed Grade, 37.6 percent Pt) in deionized and distilled water.
- An amount of CuCI 2 (Aldrich Chemical Company, Inc., 99.999 percent purity) was placed in a 250 mL Erlenmeyer flask, and the H 2 tCl6 stock solution added in an appropriate proportion with swirling to dissolve the CuCI .
- the solution was then diluted with deionized, distilled water and swirled.
- Calgon BPLF3 activated carbon (6 x 16 mesh, Calgon Carbon Corp., Pittsburgh, Pa.) was added to the flask, and the flask was agitated rapidly so that the carbon carrier was evenly coated with the aqueous Pt/Cu solution.
- the catalyst preparation was dried in an evaporating dish in air at ambient temperatures for 18 hours, and then further dried in an oven in air at 120 degrees Celsius for 2 hours.
- a catalyst charge (0.6 grams) of the thus-dried catalyst was placed in a tubular reactor within an aluminum block equipped with a cartridge heater to achieve a desired reaction temperature under computer control, over a glass wool support contained in the center of the reactor tubing. The catalyst was then covered with a plug of glass wool.
- the catalyst was dried for from 8 to 24 hours at 150 degrees Celsius under a nitrogen purge, and thereafter reduced by passing hydrogen through the reactor at a flow rate of 34 mL/minute for 24 hours.
- the reactor temperature was then adjusted to the desired temperature setpoint of 235 degrees Celsius (at 76 psig (0.52 Pa (gauge))).
- the reactor temperature and hydrogen gas flow were allowed to equilibrate for about 1 hour before the liquid 1,1,1,2-tetrachloroethane flow was started.
- the 1,1,1,2-tetrachloroethane was pumped via a high pressure syringe pump through 1/16 inch (1.6 mm) (O.D.) Monel'" nickel alloy tubing (unless specifically noted below all of the components, tubing and fittings of the test reactor apparatus were also made of Monel'" nickel alloy (Huntington Alloys, Inco Alloys International, Inc.)) into a packed sample cylinder serving as a feed evaporator.
- the 1/16th inch tubing extended almost to the center of the packed cylinder, which was heated to a vaporizing temperature of 180 degrees Celsius using electrical heat tracing.
- Vaporization of the 1,1,1,2-tetrachloroethane was accomplished in the feed line, so that the 1,1,1 ,2-tetrachloroethane was superheated when combined with the hydrogen feed stream.
- Thermocouples were used to monitor the skin temperature of the feed evaporator and the temperature of the gas exiting the feed evaporator.
- the hydrogen feed stream was metered (at a 1.6: 1 molar ratio with the 1 ,1,1 ,2- -tetrachloroethane) to a preheater using a Model 8249 linear mass flow controller from Matheson Gas Products, Inc. Secaucus, N.J., with the preheater consisting of a packed sample cylinder wrapped with electrical heat tracing. Thermocouples were used to monitor both the skin temperature of the preheater and the temperature of the gas exiting the preheater. The preheater temperature was set and maintained at 140 degrees Celsius.
- Vaporized 1 , 1 ,1 ,2-tetrachloroethane exiting the evaporator was mixed with the hydrogen gas from the preheater in a 2 foot (0.61 meter) long section of 1/4 inch (0.64 cm) tubing maintained at a temperature of 140 degrees Celsius.
- the mixed gases then were passed into and reacted within the above-mentioned tubular reactor (1/2 inch (1.27 cm) O.D., 12 inches (30.5 cm) in length).
- the residence time was 4.0 seconds.
- the products from the reaction were passed to a gas sampling valve, which provided gaseous aliquots for online gas chromatographic analysis in a Hewlett-Packard Model 5890 Series II gas chromatograph (Hewlett-Packard Company).
- the gas chromatograph was equipped with a flame ionization detector, and used 30 meter by 0.53 millimeter (I.D.) 100 percent methyl silicone/fused silica and 30 meter by 0.53 millimeter (I.D.) porous polymer-lined fused silica columns to separate the various reaction products. Response factors were conventionally determined by injections of gravimetrically-prepared standards of the individual reaction products.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Saccharide Compounds (AREA)
- Processing Of Solid Wastes (AREA)
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US95517392A | 1992-10-01 | 1992-10-01 | |
US955173 | 1992-10-01 | ||
PCT/US1993/007614 WO1994007820A1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,1,1,2-tetrachloroethane to vinylidene chloride |
CN93121102A CN1103394A (zh) | 1992-10-01 | 1993-11-30 | 1,2-二氯丙烷转化为丙烯的方法 |
CN93121101A CN1103395A (zh) | 1992-10-01 | 1993-11-30 | 氯化副产物和废产物转化为有用材料的方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0662938A1 true EP0662938A1 (en) | 1995-07-19 |
Family
ID=36940004
Family Applications (6)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93920059A Expired - Lifetime EP0662940B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,1,2-trichloroethane to vinyl chloride and/or ethylene |
EP93918729A Expired - Lifetime EP0662936B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 2-chloropropane to propylene |
EP93920061A Expired - Lifetime EP0662937B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,2-dichloropropane to propylene |
EP93920024A Ceased EP0662938A1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,1,1,2-tetrachloroethane to vinylidene chloride |
EP93920064A Expired - Lifetime EP0662941B1 (en) | 1992-10-01 | 1993-08-13 | Processes for converting chlorinated alkane byproducts or waste products to useful, less chlorinated alkenes |
EP93920025A Ceased EP0662939A1 (en) | 1992-10-01 | 1993-08-13 | Processes for converting 1,2,3-trichloropropane to allyl chloride and propylene |
Family Applications Before (3)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93920059A Expired - Lifetime EP0662940B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,1,2-trichloroethane to vinyl chloride and/or ethylene |
EP93918729A Expired - Lifetime EP0662936B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 2-chloropropane to propylene |
EP93920061A Expired - Lifetime EP0662937B1 (en) | 1992-10-01 | 1993-08-13 | Process for converting 1,2-dichloropropane to propylene |
Family Applications After (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93920064A Expired - Lifetime EP0662941B1 (en) | 1992-10-01 | 1993-08-13 | Processes for converting chlorinated alkane byproducts or waste products to useful, less chlorinated alkenes |
EP93920025A Ceased EP0662939A1 (en) | 1992-10-01 | 1993-08-13 | Processes for converting 1,2,3-trichloropropane to allyl chloride and propylene |
Country Status (8)
Country | Link |
---|---|
EP (6) | EP0662940B1 (zh) |
JP (6) | JPH08502063A (zh) |
CN (2) | CN1103395A (zh) |
AT (4) | ATE159508T1 (zh) |
AU (13) | AU5011493A (zh) |
DE (4) | DE69315703T2 (zh) |
ES (2) | ES2111770T3 (zh) |
WO (13) | WO1994007823A1 (zh) |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5447896A (en) * | 1992-06-23 | 1995-09-05 | E. I. Du Pont De Nemours And Company | Hydrodehalogenation catalysts and their preparation and use |
US5453557A (en) * | 1992-10-01 | 1995-09-26 | The Dow Chemical Company | Processes for converting chlorinated byproducts and waste products to useful materials |
US5476979A (en) * | 1992-10-01 | 1995-12-19 | The Dow Chemical Company | Processes for converting chlorinated alkenes to useful, less chlorinated alkenes |
FR2727405A1 (fr) * | 1994-11-24 | 1996-05-31 | Solvay | Procede de conversion d'alcanes chlores en alcenes moins chlores |
CN1051071C (zh) * | 1994-11-24 | 2000-04-05 | 索尔维公司 | 将氯代烷转化为较低度氯代的烯烃的方法 |
EP0714875A1 (en) * | 1994-11-28 | 1996-06-05 | The Dow Chemical Company | Hydrogenation of halogenated compounds |
BE1009400A3 (fr) * | 1995-05-24 | 1997-03-04 | Solvay | Procede de preparation d'un catalyseur et son utilisation pour la conversion d'alcanes chlores en alcenes moins chlores. |
US5637548A (en) * | 1995-07-07 | 1997-06-10 | The Dow Chemical Company | Preparation of bimetallic catalysts for hydrodechlorination of chlorinated hydrocarbons |
WO2012104365A2 (en) | 2011-02-04 | 2012-08-09 | Solvay Specialty Polymers Italy S.P.A. | Method for manufacturing perfluorovinylethers |
CN103191760B (zh) * | 2013-04-25 | 2015-10-28 | 新疆天业(集团)有限公司 | 一种乙炔氢氯化低含量金复配催化剂 |
CN103721368B (zh) * | 2014-01-02 | 2016-08-03 | 东南大学 | 一种三氯乙烯加氢脱氯的方法 |
CN105732287B (zh) * | 2016-02-03 | 2018-06-08 | 扬州大学 | 一种丙烯的制备方法 |
FR3049599B1 (fr) * | 2016-04-04 | 2018-03-16 | Arkema France | Procede de preparation de l'hexafluorobutadiene. |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2886605A (en) * | 1954-10-11 | 1959-05-12 | Dow Chemical Co | Method of reducing the halogen content of halohydrocarbons |
DE2164074C3 (de) * | 1971-12-23 | 1974-10-10 | Bayer Ag, 5090 Leverkusen | Verfahren zum Dehydrochlorieren von Chlorkohlenwasserstoffen |
GB2008583B (en) * | 1977-11-25 | 1982-03-17 | Ici Ltd | Process for the manufacture of chloroethylenes and chloroethylenes manufactured by the process |
DE2819209A1 (de) * | 1978-05-02 | 1979-11-08 | Wacker Chemie Gmbh | Katalysator und verfahren zur herstellung von trichloraethylen |
EP0015665B1 (en) * | 1979-03-02 | 1982-09-01 | Imperial Chemical Industries Plc | Manufacture of vinyl chloride |
DD235630A1 (de) * | 1985-03-25 | 1986-05-14 | Buna Chem Werke Veb | Verfahren zur herstellung von propen aus 1,2-dichlorpropan |
DE3804265A1 (de) * | 1988-02-11 | 1989-08-24 | Wacker Chemie Gmbh | Verfahren zur herstellung von trichlorethylen |
DE3941037A1 (de) * | 1989-12-12 | 1991-06-13 | Wacker Chemie Gmbh | Verfahren zur herstellung von trichlorethylen |
FR2661671B1 (fr) * | 1990-05-03 | 1992-07-17 | Atochem | Procede de dechloration des chloromethanes superieures. |
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1993
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- 1993-08-13 AT AT93920064T patent/ATE161004T1/de not_active IP Right Cessation
- 1993-08-13 AU AU50087/93A patent/AU5008793A/en not_active Abandoned
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