CN100338001C - Production of 1,1,1,2-tetrafluoroethykane and pentafuoethane simultaneously - Google Patents
Production of 1,1,1,2-tetrafluoroethykane and pentafuoethane simultaneously Download PDFInfo
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- CN100338001C CN100338001C CNB2004100945939A CN200410094593A CN100338001C CN 100338001 C CN100338001 C CN 100338001C CN B2004100945939 A CNB2004100945939 A CN B2004100945939A CN 200410094593 A CN200410094593 A CN 200410094593A CN 100338001 C CN100338001 C CN 100338001C
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Abstract
The present invention relates to a method for preparing fluorine-containing alkane, particularly to a method for simultaneously preparing 1, 1, 1, 2-tetrafluoroethykane and pentafluoroethane. The present invention has the technical scheme that trichloroethylene is used as a raw material, anhydrous ferric chloride is used as a catalyst which reacts with Cl2 to partially generate pentachloroethane, then a mixture of antimony pentachloride and anhydrous ferric trichloride is used as a catalyst which reacts with HF to generate the mixture of 1, 1, 1-trifluoro-2-chloroethane and 1, 1, 1, 2-tetrafluoro-2-chloroethane, a mixture of CrF3, AlF3, ZnF2 and MgF2 is used as a catalyst which reacts with HF at the temperature of 200 to 400 DEG C and under the pressure of 0 to 0.5MPa to generate a mixture of 1, 1, 1, 2-tetrafluoroethykane and pentafluoroethane, and the 1, 1, 1, 2-tetrafluoroethykane and the pentafluoroethane are obtained by separation, water washing, alkali washing, dewatering, rectification and drying. In the method of the present invention, the richloroethylene is used as the principal raw material, and the 1, 1, 1, 2-tetrafluoroethykane and the pentafluoroethane can be simultaneously obtained by a device.
Description
Technical field
The present invention relates to a kind of method for preparing fluorine-containing alkane, relate in particular to and a kind ofly prepare 1,1,1 simultaneously, the method for 2-Tetrafluoroethane and pentafluoride ethane.
Background technology
Because traditional widely used CF
2Cl
2, CHF
2Cooling agent such as Cl, R502 is chloride halogenated alkane, and chloride halogenated alkane can destroy the ozonosphere in the earth sky, thereby is limited by a series of international treaties or ban use of.The substitute that can be used as chloride halohydrocarbon cooling agent now is some not chloride fluoric ethers, as methylene fluoride (R32), 1,1,1,2-Tetrafluoroethane (R134a is hereinafter to be referred as R134a), pentafluoride ethane (R125 is hereinafter to be referred as R125) etc., particularly R134a and R125 are often simultaneously as the component of the cooling agent that is mixed.
At present R134a makes raw material with trieline (TCE is hereinafter to be referred as TCE) and anhydrous hydrogen fluoride (HF is hereinafter to be referred as HF), fluoridizes through two steps, with some knockout towers separation and make.The production method of a kind of R134a is disclosed as Chinese patent CN 1153160 A, this production method is a raw material with TCE and HF, adopt two reactors and a rectifying tower to react, adopt second stage reactor outlet product to be recycled to the method for first Reactor inlet, this method can only make R134a product, and the second step reaction conversion ratio is lower, is about 22%.
At present R125 makes raw material with zellon (PCE is hereinafter to be referred as PCE) and HF, and circulating through two step Reaction Separation makes, and for example Chinese patent CN1033989A discloses and a kind ofly fluoridized Cr with HF with PCE or pentaline (R120 is hereinafter to be referred as R120)
2O
3Produce the method for R125 as catalyzer, the R125 content in the thick in the method gas has only 10.7%, and can not make R134a and R125 simultaneously.
Japanese patent laid-open 7-324044 discloses and has a kind ofly made raw material with PCE and HF, produces the method for R125 through two reactors and two knockout towers, and thick in the method gas R125 content is 19.4%, and this method can not make R134a and R125 simultaneously.
Chinese patent CN1268501A discloses and has a kind ofly made the method that raw material is produced R124 and R125 simultaneously with R123 and HF, temperature of reaction is 280 ℃ in the method, R125 content is 55.08%, R124 content is 16.82%, this method can not make R134A and R125 simultaneously, and does not disclose the manufacture method of R123 in this patent.
Summary of the invention
The objective of the invention is to make raw material, make R134a and R125 simultaneously with TCE and HF.The technical solution used in the present invention is finished in the following way:
TCE and chlorine are reacted in the presence of the FERRIC CHLORIDE ANHYDROUS catalyzer, generate R120, R120 and TCE ratio can be with leading to Cl in the resultant
2Regulate with the reaction times, the R120 that generates and TCE mixture without any second reactor of feeding that separate, are reacted with HF in the presence of antimony pentachloride and FERRIC CHLORIDE ANHYDROUS mixed catalyst, generate R133a (1,1,1-three fluoro-2-monochloroethane), R123 (1,1,1-three fluoro-2, the 2-ethylene dichloride), R124 (1,1,1,2 tetrafluoros-2-monochloroethane), R125, the chlorination reaction degree of the ratio of R133a and R123, R124, R125 by the first step regulated; The second stage reactor top is provided with knockout tower and reflux exchanger, separates the temperature and pressure of cat head by control, can make that the total content of R133a and R124 reaches more than 95% in the organism of reflux exchanger top product.Separate with dry method and directly to enter the 3rd reactor after removing HCl, in the presence of catalysts for gas phase fluorination, under given temperature and pressure, react generation R134a and R125 with HF, telling unreacted HF, R133a and R124 through two knockout towers returns the 3rd reactor and reacts again, isolate HCl and make the hydrochloric acid byproduct, remaining material can make R134a and R125 through washing, alkali cleaning, distillation, drying.
In the method for the present invention, its reaction conditions is: the first step catalysts is a FERRIC CHLORIDE ANHYDROUS, or reduced iron powder, and temperature of reaction is 50～120 ℃, and reaction pressure is 0～1MPa, Cl
2To the TCE mol ratio is 0～7, and the reaction times is 1～20 hour.The ratio of the finished product R134a and R125 is the logical Cl of control in this step reaction
2Ratio, temperature of reaction and reaction times are regulated, if logical Cl
2Ratio is higher, and temperature of reaction is lower, and the residence time is longer, and R125 is higher in the final product, and then R134a is higher on the contrary.
The second step catalysts is the mixture of antimony pentachloride and FERRIC CHLORIDE ANHYDROUS or reduced iron powder, and wherein the content of FERRIC CHLORIDE ANHYDROUS or reduced iron powder is 0～10%, and temperature of reaction is 50～120 ℃, and pressure is 0.01～1.5MPa.HF is 3～10 to the organic matter raw material mol ratio, and reaction time is 1～20 hour.
The three-step reaction catalyzer is the mixture of chromium fluoride, aluminum fluoride, zinc fluoride, magnesium fluoride, and its content respectively is 50～97%, 1～70%, 0.5～20%, 0.1～10%.Its manufacturing step is water-soluble salt such as the nitrate or the muriatic aqueous solution with Al, Cr, Zn, Mg, add the ammoniacal liquor co-precipitation and make mixed hydroxides, adding an amount of binding agent and suitable quantity of water behind drying, the ball milling mixes, extrusion molding, logical at a certain temperature HF gas activation makes major part transform into fluorochemical after the oven dry.
The three-step reaction temperature is 250～400 ℃, and reaction pressure is 0～0.5MPa, and the residence time is 5～100 seconds, and HF is 3～10 to the mol ratio of organism.
The three-step reaction product is told unreacted raw material R133a, R124 and HF through two knockout towers, return the 3rd reactor and react, tell HCl and make byproduct hydrochloric acid, remaining mixture is R134a and R125, through washing, alkali cleaning, rectifying, drying, promptly get two kinds of products of R134a and R125.
By the inventive method, the first step reaction and the reaction of second step can be finished in same reactor.Catalyzer is the mixture of FERRIC CHLORIDE ANHYDROUS or reduced iron powder and antimony pentachloride, and reduced iron powder or FERRIC CHLORIDE ANHYDROUS content are 1%～50%, and reactor has steam-heated cal(l)andria chuck and TCE, AHF, Cl
2With the import of catalyzer, a knockout tower is arranged on the reactor, knockout tower top connects a reflux exchanger, and temperature of reaction is 50～120 ℃, and reaction pressure is 0.01～1.5MPa, and HF is 3～10 to the TCE mol ratio.Cl
2To the TCE mol ratio is 0～7, and the residence time is 1～20 hour, and the ratio of the finished product R134a and R125 can be regulated by the temperature of reaction of this step reaction, logical chlorine ratio and the residence time, if temperature of reaction is lower, and logical Cl
2Ratio is higher, and the residence time is longer, and then product R125 is higher, and then R134a is higher on the contrary.
The inventive method can be used TCE, HF and Cl
2Produce R134a and R125 in a covering device simultaneously, the ratio of R134a and R125 can be regulated, and can only produce R134a or only produce R125, or produce R134a and R125 simultaneously, and overall yield of reaction can reach 95%, can save cost of equipment and energy consumption cost, reduces raw material type.
Description of drawings
Fig. 1 makes the process flow sheet of R134a and R125 simultaneously for the first step reaction and second goes on foot reaction respectively at two reactor internal reactions.
Embodiment
Contrast accompanying drawing below, the invention will be further described.
With reference to accompanying drawing 1, TCE and Cl
2Enter reactor 1 by pipeline 11 and 12 respectively, under catalyst action, reaction is after pipeline 13 enters reactor 2, follow the HF that adds through pipeline 14 under catalyst action, to react, through knockout tower 4, reflux exchanger 5 separates, the material that comes out from reflux exchanger 5 enters knockout tower 6 through pipeline 15, tell HCl from knockout tower 6 napexes and produce byproduct hydrochloric acid, the material that comes out from knockout tower 6 bottoms is mainly R133a, R124 and a small amount of unreacted raw material HF, follow the mixing of materials of coming out in knockout tower 10 bottoms, additional HF to HF passes through vaporizer 7 through pipeline 18 after the organic phase mol ratio is reached prescribed value, enter reactor 3, the material that comes out from reactor 3 bottoms is through pipeline 19, again through condenser 8, enter knockout tower 9, tell HCl from the knockout tower top and produce byproduct hydrochloric acid, the material that comes out from the knockout tower bottom enters knockout tower 10 through pipeline 21, tell unreacted raw material R124 from knockout tower 10 bottoms, R133a and HF follow the mixing of materials that knockout tower 6 bottoms are come through pipeline 22, replenish HF after pipeline 18 reenters reactor 3 reacts again.The material that comes out from knockout tower 10 tops is mainly the mixture of R125 and R134a, can obtain R134a and R125 simultaneously respectively after washing, alkali cleaning, rectifying, drying.
With reference to accompanying drawing 2, Cl
2Through pipeline 12, TCE and HF mix and enter reactor 2 through pipeline 13, react under catalyst action, and reactant, ejects the material that comes from reflux exchanger and enters knockout tower 6 through pipeline 15 with after reflux exchanger 5 separates through knockout tower 4, below follows accompanying drawing 1 identical.
Below by embodiment the present invention is done further concrete the elaboration, but be not limited.
Embodiment 1:
The first step reaction and the reaction of second step are respectively at two reactor internal reactions, and the production technique of making R134a and R125 simultaneously is:
1, No. 1 Preparation of catalysts.Add 732.5g (500ml) TCE in one 1 liter four-hole boiling flask, the 50g reduced iron powder is loaded onto reinforcement agitator, reflux exchanger, logical Cl
2Pipe and temperature tube are opened agitator, reflux exchanger water flowing cooling, and the four-hole boiling flask heating in water bath, temperature is 70 ℃ in the control flask, logical then Cl
2Reaction, reflux exchanger pushes up unreacted Cl
2Guide in 10% sodium hydroxide solution and absorb logical Cl
2Speed is about 0.5 liter/minute, directly causes the reduced iron powder total overall reaction, promptly obtains the halohydrocarbon solution of FERRIC CHLORIDE ANHYDROUS, wherein contains FeCl in this solution
315.30%, this solution is catalyzer No. 1.
2, No. 2 Preparation of catalysts.No. 1 catalyzer of 32.6g added to mix in the 95g antimony pentachloride make it dissolving and promptly get catalyzer No. 2, wherein in No. 2 catalyzer, FeCl
3Be 3.90%; SbCl
5Be 74.45%; R120 is 21.65%.
3, No. 3 Preparation of catalysts.With 400g Cr (NO
3)
39H
2O, 75g Al (NO
3)
39H
2O, 42gZn (NO
3)
26H
2O, 13gMg (NO
3)
26H
2O is dissolved in two liters of pure water, promptly gets A liquid; Prepare 0.36 liter of 28% ammoniacal liquor, promptly get B liquid; In the reactor of belt stirrer, add one liter of pure water, start agitator, drip A liquid and B liquid under the room temperature simultaneously, adjust both rate of addition and make reaction solution pH in 8～10 scopes, drip off in two hours, aging 24 hours of precipitation, filter, with the pure water washing, filter cake was in 120 ℃ of dryings 24 hours, add 2% graphite, ball milling 4 hours adds the suitable quantity of water extrusion molding, become the Cylinder of diameter 3mm, length 5mm, in 120 ℃ of dryings 24 hours, place the reaction tubes of carbon steel system, logical N
2, be heated to 200 ℃, logical HF activation, the HF flow increases gradually, N
2Flow reduces gradually, stops logical N at last
2, all logical HF is warming up to 400 ℃ and continues logical HF activation 4 hours, is cooled to room temperature, logical N
2Expulsion HF promptly gets catalyzer No. 3.
4, press the technical process advancing equipment of accompanying drawing 1, wherein reactor 1 volume is 4 liters, and reactor 2 volumes are 4 liters, and reactor 3 volumes are 1.6 liters.In reactor 1, add 2.7 liters of TCE and 0.27 liter of No. 1 catalyzer, add 1.5 liters of No. 2 catalyzer in the reactor 2, add No. 3 catalyzer of 1Kg in the reactor 3.70 ℃ of reactor 1 temperature, pressure is gauge pressure 0.1MPa; 90 ℃ of reactor 2 temperature, pressure is gauge pressure 0.4MPa; 300 ℃ of reactor 3 temperature, pressure is gauge pressure 0.01MPa.The first reactor TCE rate of feeding is 700g/h, Cl
2To the TCE mol ratio is 2.2.The second reactor HF is 3.3 to the TCE molar ratio.The 3rd reactor HF is 8 to the organic raw material molar ratio.The stable back of question response from export 13, outlet 15, outlet 19 and export 23 draw sampless and wash laggard promoting the circulation of qi analysis of hplc through 10%NaOH, the result is as shown in table 1.
Embodiment 2:
The first step reaction and second step are reflected in the same reactor finishes, and the production technique of making R134a and R125 simultaneously is:
1, No. 1 Preparation of catalysts.No. 1 Preparation of catalysts is identical with method among the embodiment 1.
2, No. 2 Preparation of catalysts.No. 2 Preparation of catalysts are identical with method among the embodiment 1.
3, No. 3 Preparation of catalysts.No. 3 Preparation of catalysts are identical with method among the embodiment 1.
4, press the technical process advancing equipment of accompanying drawing 2, wherein, the first step reaction and the reaction of second step are all reacted in reactor 2, and No. 1 catalyzer of adding is 0.3 liter in the reactor 2,1.4 liters of No. 2 catalyzer; The TCE rate of feeding is 700g/h, Cl
2To the TCE mol ratio is 1.5; Reactor 2HF is 3.3 to the TCE molar ratio; No. 3 reactor HF is 9 to the organism molar ratio.Other is identical with embodiment 4.The stable back of question response from export 15, outlet 19 and export 23 draw sampless and wash laggard promoting the circulation of qi analysis of hplc through 10%NaOH, the result is as shown in table 1.
Table 1 (peak area %)
| Embodiment | Thief hole | R115 | R125 | R134a | R124 | R133a | R123 | R123a | R120 | TCE |
| 1 | 13 | / | / | / | / | / | / | / | 88.31 | 10.60 |
| 15 | 0.01 | 1.82 | / | 85.36 | 9.42 | 3.10 | 0.05 | / | / | |
| 19 | 0.23 | 58.19 | 4.41 | 28.15 | 6.73 | 2.07 | / | / | / | |
| 23 | 0.49 | 86.34 | 11.14 | 1.24 | 0.79 | / | / | / | / | |
| 2 | 15 | 0.01 | 6.21 | / | 20.25 | 69.31 | 4.09 | / | / | / |
| 19 | 0.21 | 19.57 | 20.80 | 9.53 | 47.43 | 2.24 | / | / | / | |
| 23 | 0.34 | 46.09 | 51.35 | 1.17 | 0.53 | / | / | / | / |
Claims (10)
1, a kind ofly prepare 1 simultaneously, 1,1, the method of 2-Tetrafluoroethane and pentafluoride ethane is characterized in that reaction divided for three steps, and the first step is reflected at catalyzer and exists down, trieline is with chlorine reaction, part generates pentaline, and the reaction of second step is a trieline in the presence of catalyzer, pentaline and hydrogen fluoride reaction generate 1,1,1-three fluoro-2-monochloroethane and 1,1,1,2-tetrafluoro-2-monochloroethane and hydrogenchloride, three-step reaction is that the product of the second step reaction reacts and obtains 1 removing de-chlorine hydride heel hydrogen fluoride gas phase in the presence of catalyzer, 1,1,2-Tetrafluoroethane and pentafluoride ethane mixture, make 1 through rectifying separation, 1,1, two kinds of products of 2-Tetrafluoroethane and pentafluoride ethane.
2, according to claim 1ly a kind ofly prepare 1,1,1 simultaneously, the method for 2-Tetrafluoroethane and pentafluoride ethane is characterized in that the first step catalysts is FERRIC CHLORIDE ANHYDROUS or reduced iron powder.
3, according to claim 1ly a kind ofly prepare 1,1,1 simultaneously, the method for 2-Tetrafluoroethane and pentafluoride ethane is characterized in that the first step temperature of reaction is 50 ℃～120 ℃, and reaction pressure is 0～1MPa, Cl
2To the trieline mol ratio is 2.2～7, and the residence time is 1～20 hour.
4, according to claim 1ly a kind ofly prepare 1 simultaneously, 1,1, the method for 2-Tetrafluoroethane and pentafluoride ethane, it is characterized in that the second step catalysts is the mixture of antimony pentachloride and FERRIC CHLORIDE ANHYDROUS or reduced iron powder, the content of FERRIC CHLORIDE ANHYDROUS or reduced iron powder is 0～10%.
5, according to claim 1ly a kind ofly prepare 1,1,1 simultaneously, the method of 2-Tetrafluoroethane and pentafluoride ethane is characterized in that the second step temperature of reaction is 50～120 ℃, and pressure is 0.01～1.5MPa, HF is 3～10 to the organic matter raw material mol ratio, and the residence time is 1～20 hour.
6, according to claim 1ly a kind ofly prepare 1 simultaneously, 1,1, the method of 2-Tetrafluoroethane and pentafluoride ethane, the catalyzer that it is characterized in that three-step reaction is the mixture of chromium fluoride, aluminum fluoride, zinc fluoride, magnesium fluoride, its content respectively is 50～97%, 1～70%, 0.5～20%, 0.1～10%, all components content sum equals 100%.
7, according to claim 1ly a kind ofly prepare 1,1,1 simultaneously, the method of 2-Tetrafluoroethane and pentafluoride ethane is characterized in that the three-step reaction temperature is 250～400 ℃, and reaction pressure is 0～0.5MPa, the residence time is 5～100 seconds, and HF is 3～10 to the organism mol ratio.
8, according to claim 1ly a kind ofly prepare 1 simultaneously, 1,1, the method of 2-Tetrafluoroethane and pentafluoride ethane, it is characterized in that on the second step reaction response device knockout tower and reflux exchanger being set, unreacted raw material and intermediate Returning reactor are reacted again, and the reactant that comes out from condenser overhead drops into three-step reaction after separation removes de-chlorine hydride.
9, according to claim 1ly a kind ofly prepare 1,1,1 simultaneously, the method for 2-Tetrafluoroethane and pentafluoride ethane is characterized in that material that three-step reaction comes out through knockout tower, tells the unreacted material, and the circulation Returning reactor reacts again.
10, according to claim 1ly a kind ofly prepare 1 simultaneously, 1,1, the method of 2-Tetrafluoroethane and pentafluoride ethane, it is characterized in that the first step reaction and second goes on foot to be reflected in the reactor carries out, its catalyzer is the mixture of FERRIC CHLORIDE ANHYDROUS or reduced iron powder and antimony pentachloride, reduced iron powder or FERRIC CHLORIDE ANHYDROUS content are 1%～50%, reactor top is provided with knockout tower and reflux exchanger, reactor is provided with heating jacket and trieline, anhydrous hydrogen fluoride, the import of chlorine and catalyzer, temperature of reaction are 50～120 ℃, and reaction pressure is 0.01～1.5Mpa, HF is to trieline mol ratio 3～10, Cl
2To the trieline mol ratio is 1.5～7, and the residence time is 1～20 hour.
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| CN101891583A (en) * | 2010-07-20 | 2010-11-24 | 阿拉善达康三四氯乙烯有限公司 | Method for co-production of trichloroethylene and tetrachloroethylene by gas phase catalysis method |
| CN102698779B (en) * | 2012-06-15 | 2013-11-06 | 浙江师范大学 | Catalyst for co-producing HCFC-123, HCFC-124 and HFC-125 and preparation method |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047490A (en) * | 1989-05-26 | 1990-12-05 | 阿托化学公司 | The method of synthesizing unsym.-tetraehloroethane by the hydrochlorinate of trieline |
| CN1101337A (en) * | 1993-01-27 | 1995-04-12 | 埃勒夫阿托化学有限公司 | Process for the manufacture of 1,1,1,2-tetrafluoro-2-chloroethane and of pentafluoroethane |
| CN1101338A (en) * | 1993-01-27 | 1995-04-12 | 埃勒夫阿托化学有限公司 | Process for fluorination of perchloroethylene or of pentachloroethane |
| US5659094A (en) * | 1995-08-23 | 1997-08-19 | Korea Institute Of Science And Technology | Process for co-producing 1,1,1,2-tetrafluoroethane pentafluoroethane and 1,1,1-trifluoroethane |
| JPH107603A (en) * | 1996-06-24 | 1998-01-13 | Showa Denko Kk | Production of hydrofluorocarbons |
| US5723700A (en) * | 1996-04-23 | 1998-03-03 | Korea Institute Of Science And Technology | Method for concurrently producing 1,1,1,2-tetrafluoroethane and pentafluoroethane |
| CN1205246A (en) * | 1998-07-16 | 1999-01-20 | 中国科学院上海有机化学研究所 | Catalyst for preparing 1,1,1-trifluoro-2-ethane chloride and its application |
| CN1315312A (en) * | 2000-03-09 | 2001-10-03 | 奥西蒙特股份有限公司 | Process for preparing high-purity HFC-125 |
| CN1405130A (en) * | 2001-08-03 | 2003-03-26 | 阿托菲纳公司 | Method for preparing 1,1,1,-trifluro-2,2-dichloroethane |
| WO2004018394A2 (en) * | 2002-08-23 | 2004-03-04 | Solvay (Société Anonyme) | Pentafluoroethane production method |
-
2004
- 2004-11-17 CN CNB2004100945939A patent/CN100338001C/en not_active Expired - Fee Related
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047490A (en) * | 1989-05-26 | 1990-12-05 | 阿托化学公司 | The method of synthesizing unsym.-tetraehloroethane by the hydrochlorinate of trieline |
| CN1101337A (en) * | 1993-01-27 | 1995-04-12 | 埃勒夫阿托化学有限公司 | Process for the manufacture of 1,1,1,2-tetrafluoro-2-chloroethane and of pentafluoroethane |
| CN1101338A (en) * | 1993-01-27 | 1995-04-12 | 埃勒夫阿托化学有限公司 | Process for fluorination of perchloroethylene or of pentachloroethane |
| US5659094A (en) * | 1995-08-23 | 1997-08-19 | Korea Institute Of Science And Technology | Process for co-producing 1,1,1,2-tetrafluoroethane pentafluoroethane and 1,1,1-trifluoroethane |
| US5723700A (en) * | 1996-04-23 | 1998-03-03 | Korea Institute Of Science And Technology | Method for concurrently producing 1,1,1,2-tetrafluoroethane and pentafluoroethane |
| JPH107603A (en) * | 1996-06-24 | 1998-01-13 | Showa Denko Kk | Production of hydrofluorocarbons |
| CN1205246A (en) * | 1998-07-16 | 1999-01-20 | 中国科学院上海有机化学研究所 | Catalyst for preparing 1,1,1-trifluoro-2-ethane chloride and its application |
| CN1315312A (en) * | 2000-03-09 | 2001-10-03 | 奥西蒙特股份有限公司 | Process for preparing high-purity HFC-125 |
| CN1405130A (en) * | 2001-08-03 | 2003-03-26 | 阿托菲纳公司 | Method for preparing 1,1,1,-trifluro-2,2-dichloroethane |
| WO2004018394A2 (en) * | 2002-08-23 | 2004-03-04 | Solvay (Société Anonyme) | Pentafluoroethane production method |
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