US20170166501A1 - New green preparation method for trifluorochloroethylene - Google Patents
New green preparation method for trifluorochloroethylene Download PDFInfo
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- US20170166501A1 US20170166501A1 US15/325,895 US201415325895A US2017166501A1 US 20170166501 A1 US20170166501 A1 US 20170166501A1 US 201415325895 A US201415325895 A US 201415325895A US 2017166501 A1 US2017166501 A1 US 2017166501A1
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- United States
- Prior art keywords
- trifluorochloroethylene
- tubular reactor
- zinc
- catalyst
- trihydride
- Prior art date
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- UUAGAQFQZIEFAH-UHFFFAOYSA-N chlorotrifluoroethylene Chemical group FC(F)=C(F)Cl UUAGAQFQZIEFAH-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000002360 preparation method Methods 0.000 title 1
- -1 potassium zinc trihydride Chemical compound 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 18
- 239000001257 hydrogen Substances 0.000 claims abstract description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 claims abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 11
- AJDIZQLSFPQPEY-UHFFFAOYSA-N 1,1,2-Trichlorotrifluoroethane Chemical compound FC(F)(Cl)C(F)(Cl)Cl AJDIZQLSFPQPEY-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 3
- 230000004913 activation Effects 0.000 claims description 6
- 230000003213 activating effect Effects 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 10
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 abstract description 6
- 238000006298 dechlorination reaction Methods 0.000 abstract description 6
- 229910000510 noble metal Inorganic materials 0.000 abstract description 2
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 18
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 11
- 235000005074 zinc chloride Nutrition 0.000 description 9
- 239000011592 zinc chloride Substances 0.000 description 9
- 235000011164 potassium chloride Nutrition 0.000 description 8
- 239000001103 potassium chloride Substances 0.000 description 8
- 239000008367 deionised water Substances 0.000 description 7
- 229910021641 deionized water Inorganic materials 0.000 description 7
- 150000002431 hydrogen Chemical class 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 239000003513 alkali Substances 0.000 description 6
- 239000002808 molecular sieve Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 6
- 229910000990 Ni alloy Inorganic materials 0.000 description 3
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 229910052731 fluorine Inorganic materials 0.000 description 2
- 239000011737 fluorine Substances 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- BOSAWIQFTJIYIS-UHFFFAOYSA-N 1,1,1-trichloro-2,2,2-trifluoroethane Chemical compound FC(F)(F)C(Cl)(Cl)Cl BOSAWIQFTJIYIS-UHFFFAOYSA-N 0.000 description 1
- MIZLGWKEZAPEFJ-UHFFFAOYSA-N 1,1,2-trifluoroethene Chemical group FC=C(F)F MIZLGWKEZAPEFJ-UHFFFAOYSA-N 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005538 encapsulation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 1
- 239000012761 high-performance material Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229920006280 packaging film Polymers 0.000 description 1
- 239000012785 packaging film Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- C07C21/18—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds containing fluorine
-
- 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
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
- B01J31/121—Metal hydrides
-
- 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
-
- 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
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
Definitions
- the present invention relates to a process for preparing a compound, in particular, to a process for preparing trifluorochloroethylene.
- Trifluorochloroethylene is an important special monomer for fluorine-containing high performance materials in which polytrifluorochloroethylene has superior oxygen isolating and low temperature resistant properties and thus is widely used in packaging films for medicine, electronics encapsulation applications and delivery tubes for low temperature materials. Additionally, fluorine-containing coatings with trifluorochloroethylene as the main monomer have superior weather resistant and corrosion resistant properties, and are widely used in building industries.
- the global annual output of trifluorochloroethylene is around 10,000 tons, and the primary process for preparing the same is to dechlorine from trifluorotrichloroethane with the action of zinc powder or hydrogen.
- the technical problem solved by the present invention is to provide a process for preparing trifluorochloroethylene, which is green, of low cost but high yield.
- the technical solution provided in the present invention is as follows:
- a new green process for preparing trifluorochloroethylene comprising: in a multi-tubular reactor, hydrogenation reacting 1 , 1 , 2 -trifluoro- 1 , 2 , 2 -trichloroethane directly with a catalyst potassium zinc trihydride to obtain trifluorochloroethylene, with the following chemical equation:
- the catalytic reaction is performed at a temperature of 250-350° C. and a pressure of 0.7-1.0 MPa for 10-20 seconds.
- the catalyst can be reused upon activation by addition of hydrogen, and a process for activating the catalyst comprising: activating the catalyst with the action of hydrogen, with the following chemical equation:
- the activating is performed at a temperature of 200-300° C. and a pressure of 0.9-1.0 MPa for 5-10 seconds.
- a process for preparing the catalyst potassium zinc trihydride comprising: dissolving potassium chloride in an deionized water to obtain a potassium chloride solution; dissolving zinc chloride in an deionized water to obtain a zinc chloride solution; adding dropwise the zinc chloride solution to the potassium chloride solution and reacting at 50-80° C.
- a potassium zinc trihydride solution evaporating the potassium zinc trihydride solution to obtain potassium zinc trihydride; treating the potassium zinc trihydride by hydrogenation directly using hydrogen, wherein the molar ratio of potassium zinc trihydride to hydrogen is 1:3 to 1:4, the temperature of the hydrogenation is 200-300 ° C., the reaction pressure is 0.9-1.0 MPa, and the reaction time is 5-10 seconds; the concentration of the potassium chloride solution is 20-32% by weight, the concentration of the zinc chloride is 50-82% by weight, and the conductivity of the deionized water is 0.01-0.02 ⁇ .
- the conventional process in which zinc powder is used for dechlorination or hydrogen is used for dechlorination through hydrogenation with the action of a noble metal catalyst is avoided in the process of the present invention.
- the present process substantially reduces the production cost of trifluorochloroethylene, and substantially increases the product yield, which can be up to 99% or more.
- the products obtained in the Examples of the present invention were measured by a gas chromatography/mass-spectrography 6890N/5937 (GC/MS) from Agilent.
- GC/MS gas chromatography/mass-spectrography 6890N/5937
- Potassium zinc trihydride is prepared using the following method: potassium chloride is dissolved in an deionized water (the conductivity of the deionized water is 0.01-0.02 ⁇ ) to obtain a potassium chloride solution (the concentration of the potassium chloride solution is 20-32% by weight); zinc chloride is dissolved in an deionized water (the conductivity of the deionized water is 0.01-0.02 ⁇ ) to obtain a zinc chloride solution (the concentration of the zinc chloride is 50-82% by weight); add dropwise the zinc chloride solution to the potassium chloride solution and have them react at 50-80° C.
- the potassium zinc trihydride solution is subjected to evaporation to obtain potassium zinc trihydride; the potassium zinc trihydride is then subjected to a hydrogenation treatment, wherein the molar ratio of potassium zinc trihydride to hydrogen us 1:3 to 1:4, the temperature of the hydrogenation is 200-300° C., the reaction pressure is 0.9-1.0 MPa, and the reaction time is 5-10 seconds.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes each having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L.
- the multi-tubular reactor jacket was heated with a thermal oil.
- the reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 300° C.
- 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 180 L/min.
- the pressure of the multi-tubular reactor was maintained at 0.8 MPa.
- the reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 56 Kg trifluorochloroethylene having a purity of 99.5% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.0%, and the yield was 99.20%.
- the reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 55.9 Kg trifluorochloroethylene having a purity of 99.5% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.1%, and the yield was 99.02%.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L.
- the multi-tubular reactor jacket was heated with a thermal oil.
- the reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 280° C.
- 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 120 L/min.
- the pressure of the multi-tubular reactor was maintained at 0.9 MPa.
- the reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 37.25 Kg trifluorochloroethylene having a purity of 99.60% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.2%, and the yield was 99.07%.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L.
- the multi-tubular reactor jacket was heated with a thermal oil.
- the reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 320° C.
- 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 90 L/min.
- the pressure of the multi-tubular reactor was maintained at 1.0 MPa.
- the reacted material was then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 27.85 Kg trifluorochloroethylene having a purity of 99.91% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.1%, and the yield was 99.06%.
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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)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
- The present invention relates to a process for preparing a compound, in particular, to a process for preparing trifluorochloroethylene.
- Trifluorochloroethylene (CTFE) is an important special monomer for fluorine-containing high performance materials in which polytrifluorochloroethylene has superior oxygen isolating and low temperature resistant properties and thus is widely used in packaging films for medicine, electronics encapsulation applications and delivery tubes for low temperature materials. Additionally, fluorine-containing coatings with trifluorochloroethylene as the main monomer have superior weather resistant and corrosion resistant properties, and are widely used in building industries. Currently, the global annual output of trifluorochloroethylene is around 10,000 tons, and the primary process for preparing the same is to dechlorine from trifluorotrichloroethane with the action of zinc powder or hydrogen.
- Since in the conventional process significant amount of zinc powder will be consumed when zinc powder is used for dechlorination, and meanwhile significant amount of zinc chloride waste residues will be generated, the production cost of trifluorochloroethylene would be increased a lot due to consumption of zinc powder and the need of treatment of the residues. When hydrogen is directly used for dechlorination, an expensive rare metal such as platinium, rhodium or ruthenium would be required as a catalyst, and therefore, the production cost is also relatively high. Meanwhile, hydrogenation by using hydrogen directly tends to result in excessive hydrogenation, and impurities such as trifluoroethylene may be generated, which would result in decrease of yield and purity of the product. The disadvantages of the processes disclosed in patent documents U.S. Pat. No. 2,685,606, U.S. Pat. No. 2,704,777, EP 0416015 and U.S. Pat. No. 3,333,011 have been summarized as above. Generally, the product cost of trifluorochloroethylene in these documents is relatively high, and the yield of product is relatively low, typically only about 85%.
- The technical problem solved by the present invention is to provide a process for preparing trifluorochloroethylene, which is green, of low cost but high yield. In order to solve the above technical problem, the technical solution provided in the present invention is as follows:
- A new green process for preparing trifluorochloroethylene comprising: in a multi-tubular reactor, hydrogenation reacting 1,1,2-trifluoro-1,2,2-trichloroethane directly with a catalyst potassium zinc trihydride to obtain trifluorochloroethylene, with the following chemical equation:
-
3CF2ClCCl2F+KZnH3→3ClFC=CF2+KZnCl3+3HCl, - wherein the catalytic reaction is performed at a temperature of 250-350° C. and a pressure of 0.7-1.0 MPa for 10-20 seconds.
- The catalyst can be reused upon activation by addition of hydrogen, and a process for activating the catalyst comprising: activating the catalyst with the action of hydrogen, with the following chemical equation:
-
KZnCl3+3H2→KZnH3+3HCl, - wherein the activating is performed at a temperature of 200-300° C. and a pressure of 0.9-1.0 MPa for 5-10 seconds.
- A process for preparing the catalyst potassium zinc trihydride comprising: dissolving potassium chloride in an deionized water to obtain a potassium chloride solution; dissolving zinc chloride in an deionized water to obtain a zinc chloride solution; adding dropwise the zinc chloride solution to the potassium chloride solution and reacting at 50-80° C. and atmosphere pressure for 5-10 hours to obtain a potassium zinc trihydride solution; evaporating the potassium zinc trihydride solution to obtain potassium zinc trihydride; treating the potassium zinc trihydride by hydrogenation directly using hydrogen, wherein the molar ratio of potassium zinc trihydride to hydrogen is 1:3 to 1:4, the temperature of the hydrogenation is 200-300 ° C., the reaction pressure is 0.9-1.0 MPa, and the reaction time is 5-10 seconds; the concentration of the potassium chloride solution is 20-32% by weight, the concentration of the zinc chloride is 50-82% by weight, and the conductivity of the deionized water is 0.01-0.02μ.
- The conventional process in which zinc powder is used for dechlorination or hydrogen is used for dechlorination through hydrogenation with the action of a noble metal catalyst is avoided in the process of the present invention. The present process substantially reduces the production cost of trifluorochloroethylene, and substantially increases the product yield, which can be up to 99% or more.
- The products obtained in the Examples of the present invention were measured by a gas chromatography/mass-spectrography 6890N/5937 (GC/MS) from Agilent.
- Potassium zinc trihydride is prepared using the following method: potassium chloride is dissolved in an deionized water (the conductivity of the deionized water is 0.01-0.02μ) to obtain a potassium chloride solution (the concentration of the potassium chloride solution is 20-32% by weight); zinc chloride is dissolved in an deionized water (the conductivity of the deionized water is 0.01-0.02μ) to obtain a zinc chloride solution (the concentration of the zinc chloride is 50-82% by weight); add dropwise the zinc chloride solution to the potassium chloride solution and have them react at 50-80° C. and atmosphere pressure for 5-10 hours to obtain a potassium zinc trihydride solution; the potassium zinc trihydride solution is subjected to evaporation to obtain potassium zinc trihydride; the potassium zinc trihydride is then subjected to a hydrogenation treatment, wherein the molar ratio of potassium zinc trihydride to hydrogen us 1:3 to 1:4, the temperature of the hydrogenation is 200-300° C., the reaction pressure is 0.9-1.0 MPa, and the reaction time is 5-10 seconds.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes each having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L. The multi-tubular reactor jacket was heated with a thermal oil. The reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 300° C. 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 180 L/min. The pressure of the multi-tubular reactor was maintained at 0.8 MPa. The reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 56 Kg trifluorochloroethylene having a purity of 99.5% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.0%, and the yield was 99.20%.
- When the conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane and the yield began to decrease, stop feeding and began to feed hydrogen, with the temperature of the multi-tubular reactor being maintained at 300° C., the feeding rate of hydrogen under standard state being 360 L/min, and the pressure of the multi-tubular reactor being maintained at 0.9 MPa. After 30 minutes, the activation was completed, and the feeding was switched back. The feeding rate of 1,1,2-trifluo-1,2,2-trichloroethane was 180 L/min under standard state, and the pressure of the multi-tubular reactor was maintained at 0.8 MPa. The reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 55.9 Kg trifluorochloroethylene having a purity of 99.5% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.1%, and the yield was 99.02%.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L. The multi-tubular reactor jacket was heated with a thermal oil. The reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 280° C. 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 120 L/min. The pressure of the multi-tubular reactor was maintained at 0.9 MPa. The reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 37.25 Kg trifluorochloroethylene having a purity of 99.60% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.2%, and the yield was 99.07%.
- When the conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane and the yield began to decrease, stop feeding and began to feed hydrogen, with the temperature of the multi-tubular reactor being maintained at 280° C., the feeding rate of hydrogen under standard state being 240 L/min, and the pressure of the multi-tubular reactor being maintained at 1.0 MPa. After 30 minutes, the activation was completed, and the feeding was switched back. The feeding rate of 1,1,2-trifluo-1,2,2-trichloroethane was 120 L/min under standard state, and the pressure of the multi-tubular reactor was maintained at 0.9 MPa. The reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 37.22 Kg trifluorochloroethylene having a purity of 99.70% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.2%, and the yield was 99.09%.
- 21.4 Kg potassium zinc trihydride was placed in a multi-tubular reactor comprising six nickel alloy tubes having a diameter of 40 mm and a length of 6,000 mm, and the catalyst was added in a volume of 30 L. The multi-tubular reactor jacket was heated with a thermal oil. The reactor was heated up to 250° C., and nitrogen was introduced at a rate of 10 L/min to further dry the catalyst. The introduction of nitrogen was continued for 5 hours, and then the reactor was further heated up to 320° C. 1,1,2-trifluo-1,2,2-trichloroethane was preheated and then fed into the multi-tubular reactor from the top thereof, with the feeding rate under standard state being 90 L/min. The pressure of the multi-tubular reactor was maintained at 1.0 MPa. The reacted materials were then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 27.90 Kg trifluorochloroethylene having a purity of 99.9% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.5%, and the yield was 99.22%.
- When the conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane and the yield began to decrease, stop feeding and began to feed hydrogen, with the temperature of the multi-tubular reactor being decreased to 300° C., the feeding rate of hydrogen under standard state being 180 L/min, and the pressure of the multi-tubular reactor being maintained at 0.9 MPa. After 30 minutes, the activation was completed, and the feeding was switched back. The feeding rate of 1,1,2-trifluo-1,2,2-trichloroethane was 90 L/min under standard state, and the pressure of the multi-tubular reactor was maintained at 1.0 MPa. The reacted material was then discharged from the bottom of the multi-tubular reactor, washed directly with water and alkali, dried with a molecular sieve, condensed, collected by rectification, and then samples were taken and analyzed. After an hour, 27.85 Kg trifluorochloroethylene having a purity of 99.91% was obtained. The conversion ratio of 1,1,2-trifluo-1,2,2-trichloroethane was 99.1%, and the yield was 99.06%.
- The Examples as set forth above should not be construed as limiting the present invention in any way. It should be understood that any technical solutions obtained by equivalent substitutions or variations would fall within the scope of the present invention. application:
Claims (3)
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
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CN201410339377.XA CN104140356B (en) | 2014-07-16 | 2014-07-16 | A kind of preparation method of novel green trifluorochloroethylene |
CN201410339377 | 2014-07-16 | ||
CN201410339377.X | 2014-07-16 | ||
PCT/CN2014/093346 WO2016008257A1 (en) | 2014-07-16 | 2014-12-09 | New green preparation method for trifluorochloroethylene |
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US20170166501A1 true US20170166501A1 (en) | 2017-06-15 |
US9682907B1 US9682907B1 (en) | 2017-06-20 |
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US15/325,895 Active US9682907B1 (en) | 2014-07-16 | 2014-12-09 | Green preparation method for trifluorochloroethylene |
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CN107540518B (en) * | 2016-06-27 | 2021-02-23 | 浙江蓝天环保高科技股份有限公司 | Hydrogen recycling method in production process of chlorotrifluoroethylene |
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US2685606A (en) | 1953-02-25 | 1954-08-03 | Union Carbide & Carbon Corp | Preparation of halogenated olefines |
US2704777A (en) | 1955-01-25 | 1955-03-22 | Union Carbide & Carbon Corp | Preparation of halogenated olefines |
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US4226812A (en) * | 1977-11-25 | 1980-10-07 | Allied Chemical Corporation | Process for producing chlorotrifluoroethylene |
US5204083A (en) | 1988-05-23 | 1993-04-20 | Kerr-Mcgee Chemical Corporation | Process for preparing titanium dioxide |
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US20050038302A1 (en) * | 2003-08-13 | 2005-02-17 | Hedrick Vicki E. | Systems and methods for producing fluorocarbons |
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US8044251B2 (en) | 2009-04-17 | 2011-10-25 | E. I. Du Pont De Nemours And Company | Process for the preparation of halo-olefins |
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