CN109438170B - Preparation method of 2,3,3, 3-tetrafluoropropene - Google Patents
Preparation method of 2,3,3, 3-tetrafluoropropene Download PDFInfo
- Publication number
- CN109438170B CN109438170B CN201811423031.2A CN201811423031A CN109438170B CN 109438170 B CN109438170 B CN 109438170B CN 201811423031 A CN201811423031 A CN 201811423031A CN 109438170 B CN109438170 B CN 109438170B
- Authority
- CN
- China
- Prior art keywords
- reaction
- hcfc
- tetrafluoropropene
- hfo
- chloro
- 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.)
- Active
Links
Images
Classifications
-
- 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
- C07C17/278—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions of only halogenated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
- C07C17/202—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction
- C07C17/206—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction the other compound being HX
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a preparation method of 2,3,3, 3-tetrafluoropropene, 1, 1-difluoro-2-chloroethylene and chlorofluoromethane are subjected to addition reaction in the presence of a catalyst to generate 1,1, 1-trifluoro-2, 3-dichloropropane, and the 1,1, 1-trifluoro-2, 3-dichloropropane is subjected to three-path catalysis to prepare the 2,3,3, 3-tetrafluoropropene. The invention uses 1, 1-difluoro-2-chloroethylene which is harmful to human body and environment as the initial raw material, and has the effect of protecting the environment. The method adopts the continuous tubular reactor for reaction, the reaction condition is easy to control, and the equipment operation is simple; and the preparation method has the advantages of good conversion rate of each step, high yield of target products and wide industrial application prospect.
Description
Technical Field
The invention belongs to the field of chemical synthesis, and particularly relates to a preparation method of 2,3,3, 3-tetrafluoropropene.
Background
2,3,3, 3-tetrafluoropropene serving as a new-generation refrigerant has the advantages of good refrigeration effect, small greenhouse effect, short atmospheric service life, low flammability and low toxicity, can be widely applied to refrigeration appliances such as automobiles, air conditioners, refrigerators and the like, and can also be applied to the fields of fire extinguishing agents, foaming agents, grinding and polishing machines and the like. But the preparation cost of 2,3,3, 3-tetrafluoropropene is higher and the price is higher than that of similar substitutes.
US patent US7560602B2 discloses a CF3CF2CF2CHCl2Is used as raw material and is firstly hydrodechlorinated to generate CF3CF2CH3Then HF is removed to obtain 2,3,3, 3-tetrafluoropropene. The preparation method has the advantage of consuming toxic substances CF3CF2CH3The disadvantage is the low yield of 2,3,3, 3-tetrafluoropropene.
US2996555 discloses CX3CF2CH3(wherein X is F, Cl, Br) as raw material, and the method comprises the following two reaction equations: CCl3CF2CH3+3HF→CF3CF2CH3+3HCl；CF3CF2CH3→ CF3CF＝CH2+ HF to 2,3,3, 3-tetrafluoropropene. The preparation method has high conversion rate, but the catalyst CrOxFyThe preparation of (2) is difficult.
Therefore, how to produce 2,3,3, 3-tetrafluoropropene with high efficiency and low cost is an urgent problem to be solved.
Disclosure of Invention
The invention aims to provide a preparation method of 2,3,3, 3-tetrafluoropropene, which uses 2-chloro-1, 1-difluoroethylene harmful to human bodies and environment as an initial raw material and has a protection effect on the environment.
In order to solve the technical problems, the invention adopts the following technical scheme:
a preparation method of 2,3,3, 3-tetrafluoropropene is characterized by comprising the following steps:
(1) with 2-chloro-1, 1-difluoroethylene (CF)2CHCl) with Chlorofluoromethane (CH)2ClF) as a raw material, and carrying out addition reaction under the condition of a catalyst to generate an intermediate 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243 db);
(2) the intermediate 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) synthesizes 2,3,3, 3-tetrafluoropropene by three different routes, including the following route:
(a) the 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) and HF directly carry out gas phase reaction under the action of a catalyst to prepare the 2,3,3, 3-tetrafluoropropene (HFO-1234 yf).
(b) The 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) is subjected to gas phase dehydrochlorination to prepare 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf), 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf) and HF, and the 2,3,3, 3-tetrafluoropropene (HFO-1234yf) is prepared by gas phase fluorination and dechlorination under the action of a catalyst.
(c) The 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) is subjected to gas phase dehydrochlorination to prepare 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf), and the 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf) is subjected to gas phase fluorination addition to prepare 2-chloro-1, 1,1, 2-tetrafluoropropane (HCFC-244bb), and the 2-chloro-1, 1,1, 2-tetrafluoropropane (HCFC-244bb) is subjected to gas phase dehydrochlorination to prepare 2,3,3, 3-tetrafluoropropene (HFO-1234 yf).
Preferably, the catalyst used in step (1) is SbF3-SbF5-AlCl3C, wherein Sb3+、Sb5+、Al3+The molar ratio of (1: 1: 1), the reaction temperature of the addition reaction is 50-350 ℃, preferably 100-300 ℃, more preferably 150-250 ℃, the reaction pressure is 2-4 bar, and the contact time is 1-30 s, preferably 3-15 s, more preferably 5-10 s.
Preferably, the gas-phase continuous reaction in step (1) and step (2) is carried out in a tubular reactor, a single-tube staged reactor or a multi-tube series reactor can be selected, and the material of the tubular reactor is corrosion-resistant stainless steel, Monel, Hastelloy corrosion-resistant nickel-base alloy or chromium-nickel-iron alloy.
Preferably, in the route (a) in the step (2), the catalyst is Cr2O3、Cr2O3-Al2O3、 Cr2O3-Al2O3-FeCl3-MgCl2、Al2O3-ZnCl2、Cr2O3-Ni/C、Cr2O3-Ni/Al2O3Preferably Cr2O3-Al2O3-FeCl3-MgCl2、Al2O3-ZnCl2、Cr2O3-Ni/C、Cr2O3-Ni/Al2O3More preferably Cr2O3-Ni/C、Cr2O3-Ni/Al2O3Or a mixture of the two, the catalyst being prepared by a process in which one or both of co-deposition, doping and co-action are carried out, Cr2O3The mass ratio of Cr to Ni in the-Ni/C catalyst is 20: 1-20, preferably 20: 5-10, and Cr2O3-Ni/Al2O3The mass ratio of Cr to Ni in the catalyst is 20: 1-10, preferably 20: 4-6.
Preferably, in the route (a) of the step (2), the reaction pressure of the HCFC-243db gas phase fluorination reaction is 1-10 bar, preferably 4-6 bar, the molar ratio of HF to HCFC-243db is 10-50: 1, preferably 15-25: 1, the reaction temperature is 150-340 ℃, preferably 220-280 ℃, and the reaction contact time is 10-200 s, preferably 80-140 s.
Preferably, in route (b) of step (2), the catalyst used in the gas phase dehydrochlorination of HCFC-243db is CrF3Or CrOxFyOne or a mixture of two of them; the catalyst used in the fluorination process of HFO-1233xf and HF is a series of La-Cr prepared by adopting a coprecipitation method2O3、Y-Cr2O3、Co-Cr2O3、Ga-Cr2O3、Mg-Cr2O3、 Fe-Cr2O3、Zn-Cr2O3、Cr2O3-one or a mixture of several of Ni/C catalysts.
Preferably, in the path (b) of the step (2), the reaction temperature of the HCFC-243db gas-phase dehydrochlorination process is 200-350 ℃, the reaction pressure is 1-5 bar, and the reaction contact time is 30-60 s; the reaction temperature in the HF fluorination process is 280-350 ℃, the reaction pressure is 6-8 bar, the reaction contact time is 100-150 s, and the ratio of the HF feeding flow rate to the material feeding flow rate containing HFO-1233xf is 10-20: 1.
Preferably, in route (c) of step (2), the catalyst used in the gas phase dehydrochlorination of HCFC-243db is CrF3Or CrOxFyOne or a mixture of two of them; the catalyst used in the gas phase fluoridation addition process is Zn-Cr2O3、Mg-Cr2O3、Cr2O3-one or a mixture of several of Ni/C; the catalyst used in the HCFC-244bb gas phase dehydrochlorination process is CsCl/MgF2、SbF5/C、Cr2O3-one or a mixture of two of Ni/C.
Preferably, in the path (c) in the step (2), the reaction temperature of the HCFC-243db dehydrochlorination process is 200-350 ℃, the reaction pressure is 1-5 bar, and the reaction contact time is 30-60 s; the reaction temperature in the HF fluorination addition process is 200-320 ℃, the reaction pressure is 6-10 bar, the reaction contact time is 90-120 s, and the ratio of the HF feeding flow rate to the material feeding flow rate containing HFO-1233xf is 10-20: 1; the reaction temperature in the gas-phase dehydrochlorination process of HFC-244bb is 320-380 ℃, the reaction pressure is 2-10 bar, and the reaction contact time is 100-180 s.
Due to the adoption of the technical scheme, the method has the following beneficial effects:
the invention uses 1, 1-difluoro-2-chloroethylene which is harmful to human body and environment as the initial raw material, and has the effect of protecting the environment. The method adopts the continuous tubular reactor for reaction, the reaction condition is easy to control, and the equipment operation is simple; and the preparation method has the advantages of good conversion rate of each step, high yield of target products and wide industrial application prospect.
Drawings
The invention will be further described with reference to the accompanying drawings in which:
FIG. 1 is a flow diagram of the present invention for the preparation of 2,3,3, 3-tetrafluoropropene.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
The Monel tube reactor I with the length of 1.5m and the inner diameter of 100mm is filled with the catalyst SbF3-SbF5-AlCl3The temperature of the reactor I is set to be 220 ℃, and the pressure is set to be 4 bar; will CH2ClF and CF2And (2) mixing the two CHCl products according to a molar ratio of 10:1, introducing the mixture into a reactor I, controlling the retention time to be 10s, cooling the reaction product by circulating water at 20 ℃ to recover a liquid product, and circulating the gas product into the reactor I.
Conveying HCFC-243db to a preheater through a metering pump, then feeding into a vaporization mixer, and then feeding into a device filled with CrF3The length of the catalyst is 1m, and the inner diameter of the catalyst is 60mm in a reactor II of a Hastelloy corrosion-resistant nickel-based alloy pipe. The reaction temperature was controlled at 320 ℃, the reaction pressure at 5bar and the residence time at 60 s. After the reaction product is subjected to alkali washing and water washing at 40 ℃ and dried, the gaseous product HCFC-1233xf enters a Monel alloy tube reactor III with the length of 1.5m and the inner diameter of 100 mm; the catalyst filled in the reactor III is Cr2O3-Ni/C. Anhydrous HF gas is introduced into the reactor III, and the ratio of the feed flow rates of the anhydrous HF and the HCFC-1233xf is controlled to be 10: 1; the temperature in reactor III was 340 ℃, the pressure 3bar and the reaction residence time 30 s. And (3) carrying out alkali washing, water washing and rectification on the reaction product to obtain the HFO-1234 yf.
The overall conversion of the reaction was 48.2% and the yield of HFO-1234yf was 75.7% (as CF)2CHCl).
Examples 1 to 5
The catalyst SbF was introduced into a Monel tube reactor I of 1.5m length and 100mm internal diameter3-SbF5-AlCl3C, wherein Sb3+、Sb5+、Al3+In a molar ratio of 1:1:1, 2-chloro-1, 1-difluoroethylene (CF) is introduced2CHCl) with Chlorofluoromethane (CH)2ClF), and the reaction product is made into HCFC-243db after alkali washing, water washing and rectification, and the reaction conditions and the reaction results are shown in Table 1.
Table 1: preparation of HCFC-243 db.
Examples 6 to 10
HCFC-243db prepared in examples 1-5 was transferred to a preheater by means of a metering pump, and introduced into a Monel tube reactor II having a length of 1.5m and an inner diameter of 100mm, and the reactor II was filled with a catalyst Cr2O3-Ni/C, wherein the mass ratio of Cr to Ni is 2: 1. And (3) introducing anhydrous HF gas into the reactor II, and performing alkaline washing, water washing and rectification on a reaction product to obtain HFO-1234yf, wherein the reaction conditions and the reaction results are shown in Table 2.
Table 2: HFO-1234yf is prepared by step 2 (a).
The total conversion of the reactions combining example 1 and example 6 was 32.7%, the total conversion of the reactions combining example 2 and example 7 was 41.2%, the total conversion of the reactions combining example 3 and example 8 was 49.5%, the total conversion of the reactions combining example 4 and example 9 was 52.2%, and the total conversion of the reactions combining example 5 and example 10 was 53.9%.
Examples 11 to 15
HCFC-243db prepared in examples 1-5 was transferred to a preheater via a metering pump, and then into a vaporization mixer, and further into a device containing CrF3HFO-1233xf is generated in a reactor III of a Hastelloy corrosion-resistant nickel-based alloy pipe with the length of 1m and the inner diameter of 60mm of the catalyst; after the reaction product is washed by alkali and water at 40 ℃ and dried, the gaseous product HCFC-1233xf enters a Monel alloy tube reactor IV with the length of 1.5m and the inner diameter of 100mm, and the reactor IV is filled with a catalyst La-Cr2O3The reaction product is washed by alkali, washed by water and rectified to obtain HFO-1234yf, and the reaction conditions and the reaction results for generating HFO-1233xf and HFO-1234yf are shown in Table 3.
Table 3: HFO-1234yf is prepared by step 2 (b).
The total conversion of the reactions combining example 1 and example 11 was 30.2%, the total conversion of the reactions combining example 2 and example 12 was 44.6%, the total conversion of the reactions combining example 3 and example 13 was 48.2%, the total conversion of the reactions combining example 4 and example 14 was 49.7%, and the total conversion of the reactions combining example 5 and example 15 was 45.9%.
Examples 16 to 20
The gaseous HFO-1233xf prepared using the methods of examples 11-15 was passed into a Monel tube reactor V of 1.5m length and 100mm internal diameter, in which the catalyst was Zn-Cr2O3Introducing anhydrous HF gas into the reactor V, and carrying out alkali washing, water washing and drying on a reaction product at 40 ℃ to generate HFC-244 bb; introducing HFC-244bb generated in the last step into a reactor VI of a hastelloy corrosion-resistant nickel-based alloy pipe with the length of 1m and the inner diameter of 60mm, and adding a catalyst CsCl/MgF2The reaction conditions and reaction results of the reaction products after alkali washing, water washing and rectification to generate HFO-1234yf and HFC-244bb and HFO-1234yf are shown in Table 4.
Table 4: HFO-1234yf is prepared by step 2 (c).
The total conversion of the reactions combining example 1 and example 11 was 25.8%, the total conversion of the reactions combining example 2 and example 12 was 39.8%, the total conversion of the reactions combining example 3 and example 13 was 42.5%, the total conversion of the reactions combining example 4 and example 14 was 43.4%, and the total conversion of the reactions combining example 5 and example 15 was 41.1%.
The above is only a specific embodiment of the present invention, but the technical features of the present invention are not limited thereto. Any simple changes, equivalent substitutions or modifications made on the basis of the present invention to solve the same technical problems and achieve the same technical effects are all covered in the protection scope of the present invention.
Claims (4)
1. A preparation method of 2,3,3, 3-tetrafluoropropene is characterized by comprising the following steps:
(1) with 2-chloro-1, 1-difluoroethylene (CF)2CHCl) with Chlorofluoromethane (CH)2ClF) as raw material, and carrying out addition reaction under the condition of catalyst to generate intermediate 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db), wherein the catalyst is SbF3-SbF5-AlCl3C, wherein Sb3+、Sb5+、Al3+In a molar ratio of 1:1: 1;
(2) the intermediate 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) synthesizes 2,3,3, 3-tetrafluoropropene by three different routes, including the following route:
the 1,1, 1-trifluoro-2, 3-dichloropropane (HCFC-243db) is subjected to gas phase dehydrochlorination to prepare 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf), and the catalyst used in the gas phase dehydrochlorination process of HCFC-243db is CrF3Or CrOxFyOne or a mixture of two of them; 2-chloro-1, 1,1, 2-tetrafluoropropane (HCFC-244bb) is prepared by gas phase fluorination addition of 2-chloro-3, 3, 3-trifluoropropene (HFO-1233xf), and a catalyst used in the gas phase fluorination addition process is Zn-Cr2O3、Mg-Cr2O3、Cr2O3-one or a mixture of several of Ni/C; preparation of 2,3,3, 3-tetrafluoropropene (HFO-1234yf) by gas-phase dehydrochlorination of 2-chloro-1, 1,1, 2-tetrafluoropropane (HCFC-244bb), wherein the catalyst used in the gas-phase dehydrochlorination of HCFC-244bb is CsCl/MgF2。
2. The production process according to claim 1, wherein the reaction mixture comprises 2,3,3, 3-tetrafluoropropene, and the reaction mixture comprises: the reaction temperature of the addition reaction in the step (1) is 50-350 ℃, the reaction pressure is 2-4 bar, and the contact time is 1-30 s.
3. The production process according to claim 1, wherein the reaction mixture comprises 2,3,3, 3-tetrafluoropropene, and the reaction mixture comprises: the steps (1) and (2) are carried out gas phase continuous reaction in a tubular reactor, a single-tube staged reactor or a multi-tube series reactor is selected, and the tubular reactor is made of corrosion-resistant stainless steel, Monel alloy, Hastelloy corrosion-resistant nickel-based alloy or chromium-nickel-iron alloy.
4. The production process according to claim 1, wherein the reaction mixture comprises 2,3,3, 3-tetrafluoropropene, and the reaction mixture comprises: in the step (2), the reaction temperature of the HCFC-243db dehydrochlorination process is 200-350 ℃, the reaction pressure is 1-5 bar, and the reaction contact time is 30-60 s; the reaction temperature in the HF fluorination addition process is 200-320 ℃, the reaction pressure is 6-10 bar, the reaction contact time is 90-120 s, and the ratio of the HF feeding flow rate to the material feeding flow rate containing HFO-1233xf is 10-20: 1; the reaction temperature in the gas-phase dehydrochlorination process of HFC-244bb is 320-380 ℃, the reaction pressure is 2-10 bar, and the reaction contact time is 100-180 s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811423031.2A CN109438170B (en) | 2018-11-27 | 2018-11-27 | Preparation method of 2,3,3, 3-tetrafluoropropene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811423031.2A CN109438170B (en) | 2018-11-27 | 2018-11-27 | Preparation method of 2,3,3, 3-tetrafluoropropene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109438170A CN109438170A (en) | 2019-03-08 |
| CN109438170B true CN109438170B (en) | 2022-02-01 |
Family
ID=65555797
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811423031.2A Active CN109438170B (en) | 2018-11-27 | 2018-11-27 | Preparation method of 2,3,3, 3-tetrafluoropropene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109438170B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112778079A (en) * | 2019-11-05 | 2021-05-11 | 浙江环新氟材料股份有限公司 | Process for producing 2-chloro-1, 1, 1, 2-tetrafluoropropane and 2, 3, 3, 3-tetrafluoropropene |
| WO2021093029A1 (en) * | 2019-11-13 | 2021-05-20 | Fujian Yongjing Technology Co., Ltd | New process for synthesis of 2,3,3,3-tetrafluoropropene (1234yf) and 2,3-dichloro-1,1,1-trifluoropropane (243db) |
| CN113527045B (en) * | 2020-04-22 | 2023-09-26 | 浙江省化工研究院有限公司 | Preparation method of fluorophlorpropane |
| CN113527040B (en) * | 2020-04-22 | 2023-09-01 | 浙江省化工研究院有限公司 | Preparation method of halogenated propylene |
| CN115215722B (en) * | 2021-04-15 | 2023-10-03 | 浙江省化工研究院有限公司 | Co-production preparation method of 2, 3-tetrafluoropropene and 1-chloro-3, 3-trifluoropropene |
| WO2022218204A1 (en) * | 2021-04-15 | 2022-10-20 | 浙江省化工研究院有限公司 | Method for preparing 2,3,3,3-tetrafluoropropene |
| CN113943204B (en) * | 2021-10-30 | 2023-06-23 | 山东东岳化工有限公司 | Resource utilization method of pentafluoroethane |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101979364A (en) * | 2010-09-30 | 2011-02-23 | 浙江环新氟材料股份有限公司 | Method for preparing 2,3,3,3-tetrafluoropropylene |
| CN105377797A (en) * | 2013-07-12 | 2016-03-02 | 大金工业株式会社 | Method for producing 2,3,3,3-tetrafluoropropene |
| CN106008141A (en) * | 2008-09-11 | 2016-10-12 | 法国阿科玛公司 | Process for preparation of 2,3-dichloro-1,1,1-trifluoropropane and 2,3,3,3-tetrafluoroprop-1-ene |
| WO2017013406A1 (en) * | 2015-07-17 | 2017-01-26 | Mexichem Fluor S.A. De C.V. | Process for the preparation of 2,3,3,3-tetrafluoropropene (1234yf) |
| WO2018046927A1 (en) * | 2016-09-07 | 2018-03-15 | Mexichem Fluor S.A. De C.V. | Catalyst and process using the catalyst for manufacturing fluorinated hydrocarbons |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7700815B2 (en) * | 2007-09-28 | 2010-04-20 | Honeywell International Inc | Method for producing fluorinated organic compounds |
| GB0806389D0 (en) * | 2008-04-09 | 2008-05-14 | Ineos Fluor Holdings Ltd | Process |
-
2018
- 2018-11-27 CN CN201811423031.2A patent/CN109438170B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106008141A (en) * | 2008-09-11 | 2016-10-12 | 法国阿科玛公司 | Process for preparation of 2,3-dichloro-1,1,1-trifluoropropane and 2,3,3,3-tetrafluoroprop-1-ene |
| CN101979364A (en) * | 2010-09-30 | 2011-02-23 | 浙江环新氟材料股份有限公司 | Method for preparing 2,3,3,3-tetrafluoropropylene |
| CN105377797A (en) * | 2013-07-12 | 2016-03-02 | 大金工业株式会社 | Method for producing 2,3,3,3-tetrafluoropropene |
| WO2017013406A1 (en) * | 2015-07-17 | 2017-01-26 | Mexichem Fluor S.A. De C.V. | Process for the preparation of 2,3,3,3-tetrafluoropropene (1234yf) |
| WO2018046927A1 (en) * | 2016-09-07 | 2018-03-15 | Mexichem Fluor S.A. De C.V. | Catalyst and process using the catalyst for manufacturing fluorinated hydrocarbons |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109438170A (en) | 2019-03-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109438170B (en) | Preparation method of 2,3,3, 3-tetrafluoropropene | |
| CN102282114B (en) | Isomerization of 1,1,3,3-tetrafluoropropene | |
| CN101553453B (en) | Process for the manufacture of fluorinated olefins | |
| EP2178814B1 (en) | Method for producing fluorinated olefins | |
| EP3296281B1 (en) | Process for the preparation of 2,3,3,3-tetrafluoropropene | |
| CN106349005B (en) | A kind of method of coproduction trifluoropropyl alkenes product and tetrafluoropropene class product | |
| CN101687731A (en) | Process for the manufacture of hydrofluoroolefins | |
| US20120203036A9 (en) | Gas phase synthesis of 2,3,3,3-tetrafluoro-1-propene from 2-chloro-3,3,3-trifluoro-1-propene | |
| JP2019196312A (en) | Manufacturing method of 1,2-difluoroethylene and/or 1,1,2-trifluoroethane | |
| CN102001911A (en) | Method for preparing 2,3,3,3-tetrafluoropropene | |
| JP6392777B2 (en) | Method for producing 1,3,3,3-tetrafluoropropene | |
| CN110283044A (en) | The selective catalysis dehydrochlorination of hydrochlorofluorocarbons | |
| CN102001910A (en) | Method for preparing 2,3,3,3-tetrafluoropropene | |
| CN104710274B (en) | Process for co-producing 1,3,3,3-tetrafluoropropene and/or 2,3,3,3-tetrafluoropropene | |
| CN105188909A (en) | Fluorination process and reactor | |
| CN103508843B (en) | A kind of gas phase fluorination prepares the method for chloro-3,3, the 3-trifluoro propenes of 1,2-bis- | |
| ES2755791T3 (en) | Preparation procedure for the joint production of HFO-1234ze and HFC-245fa | |
| CN103041819B (en) | Catalyst for fluoridation and preparation method for same | |
| CN104159878A (en) | Process for 1,3,3,3-tetrafluoropropene | |
| WO2016019485A1 (en) | Method for preparing 2,3,3,3-tetrafluoropropene | |
| CN104496746A (en) | Method for simultaneously preparing 1,1,1,2,2-pentachloropropane and 2,3,3,3-tetrachloropropene | |
| CN109438171B (en) | Method for continuously synthesizing 2,3,3, 3-tetrafluoropropene in gas phase | |
| WO2013141409A1 (en) | Process for preparing 2-chloro-3,3,3-trifluoropropene | |
| CN111848331A (en) | Method for synthesizing 2-chloro-3, 3, 3-trifluoropropene through gas phase fluorination | |
| CN102211974A (en) | Preparation method of 1,3,3,3-tetrafluoropropylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A preparation method of 2,3,3,3-tetrafluoropropene Effective date of registration: 20220930 Granted publication date: 20220201 Pledgee: Industrial and Commercial Bank of China Limited Wuyi sub branch Pledgor: ZHEJIANG SANMEI CHEMICAL INDUSTRY CO.,LTD. Registration number: Y2022330002419 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230526 Granted publication date: 20220201 Pledgee: Industrial and Commercial Bank of China Limited Wuyi sub branch Pledgor: ZHEJIANG SANMEI CHEMICAL INDUSTRY CO.,LTD. Registration number: Y2022330002419 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| CB03 | Change of inventor or designer information |
Inventor after: Xu Qingrui Inventor after: Wang Xiaodong Inventor after: Xu Yu Inventor after: Chen Chenkai Inventor after: Wu Chenxing Inventor after: Wu Yehua Inventor after: Hu Shengwei Inventor after: Li Fei Inventor after: Zhan Linxi Inventor before: Xu Qingrui Inventor before: Wang Xiaodong Inventor before: Xu Yu Inventor before: Chen Chengkai Inventor before: Wu Chenxing Inventor before: Wu Yehua Inventor before: Hu Shengwei Inventor before: Li Fei Inventor before: Zhan Linxi |
|
| CB03 | Change of inventor or designer information |