WO1993008146A1 - Process for the manufacture of 1,1,1,2-tetrafluoroethane - Google Patents
Process for the manufacture of 1,1,1,2-tetrafluoroethane Download PDFInfo
- Publication number
- WO1993008146A1 WO1993008146A1 PCT/US1992/008924 US9208924W WO9308146A1 WO 1993008146 A1 WO1993008146 A1 WO 1993008146A1 US 9208924 W US9208924 W US 9208924W WO 9308146 A1 WO9308146 A1 WO 9308146A1
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- WIPO (PCT)
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- catalyst
- fluorination
- hfc
- cfc
- boehmite
- Prior art date
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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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/06—Halogens; Compounds thereof
- B01J27/132—Halogens; Compounds thereof with chromium, molybdenum, tungsten or polonium
-
- 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
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/24—Chromium, molybdenum or tungsten
- B01J23/26—Chromium
-
- 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
Definitions
- Fiel of the Ipverfcion This invention relates generally to the fluorination of halogenated hydrocarbons. More specifically, it relates to the fluorination with HF of l,l,l-trifluoro-2-chloroethane (CFC-133a) to produce 1,1,1,2-tetrafluoroethane (HFC-134a) , a compound likely to replace CFC-12 (dichlorodifluoromethane) in certain applications.
- CFC-133a l,l,l-trifluoro-2-chloroethane
- HFC-134a 1,1,1,2-tetrafluoroethane
- Prior Art CFC-12 is widely used in air conditioning equipment and other applications, but its use is being limited because of concern about depletion of the atmospheric ozone layer.
- Alumina is used as a support for a metal fluoride which may include chromium in O8910341-A. Chromium salts are impregnated on gamma-alumina in J02/157235A for a vapor phase reaction which produces CFC * -23 rather than HFC-134a.
- a supported chromium oxide or halide is used to make HFC-134a in J02/172933A. Chromium is supported on A1F 3 for preparation of HFC-134a in U.S. Pat. No. 4,766,260 and U.S. Pat. 5,008,475.
- the present invention particularly relates to a catalyst for such an improved process.
- the catalyst of the invention has application to other related fluorinations.
- Vaporphase fluorination of hydrocarbons and/or halogenated hydrocarbons and in particular fluorination of l,l,l-trifluoro-2-chloroethane (CFC-133a) to 1,1,1,2- tetrafluoroethane (HFC-134a) , may be carried out at fluorination conditions in the presence of HF over a catalyst produced by mixing an acidic chromium compound, preferably a chromium hydroxy chloride, Cr(OH)Cl 2 »2H 2 0 with an aluminum oxide hydrate, preferably boehmite and water, then extruding pellets and heating in nitrogen (not air) .
- an acidic chromium compound preferably a chromium hydroxy chloride, Cr(OH)Cl 2 »2H 2 0
- an aluminum oxide hydrate preferably boehmite and water
- the catalyst is prepared by mixing 95 to 9 wt.% of a finely powdered boehmite
- particles of about 10 to 75 microns with 5 to 91 wt.% of Cr(OH)Cl 2 '2H 2 0 and water to form a dough, which is then extruded to form particles suitable for use in a fixed bed reactor.
- the particles may be dried at a temperature of about 20"C to 120*C in air, preferably 70*C to 100 ⁇ C, and thereafter, heated in nitrogen at 300*C to 650°C, preferably 400"C to 550*C, and held at the maximum temperature for about 2 to 12 hours, preferably about 4 hours.
- the process may be carried out in the vapor phase with a mole ratio of HF to CFC-133a of 10/1 to 1/1.
- the mole ratio would be about 5/1 to 2/1.
- the reaction conditions include a temperature in the range of about 300*c to 450*C, preferably a temperature of about 325*C to 400*C, and a pressure in the range of 100 to 2,000 kPa, preferably about 172 to 517 kPa gauge.
- the liquid hourly space velocity will be about 0.5 to 5.0 hr * , preferably about 0.75 to 2 hr "1 . based on the feedstock.
- Figures l and 2 show the activity and selectivity of catalysts of the invention in converting CFC-133a to HFC-134a.
- the Catalyst is made from an aluminum oxide hydrate, preferably boehmite (alpha alumina monohydrate i.e., AIO(OH) or A1 2 0 3 «H 2 0) and an acidic chromium compound, preferably Cr(OH)Cl 2 »2H 2 0 since the combination has been found to provide performance similar to the CF 3 or Cr 2 0 3 catalysts of the prior art, but at substantially lower cost.
- the catalyst is the product resulting from calcining a mixture of about 95 to 9 wt.% boehmite and about 5 to 91 wt.% of Cr(OH)Cl 2 «2H 2 0.
- the mixture will contain about 90 to 65 wt.% boehmite and about .. ⁇ > to 10 wt.% of Cr(OH)Cl 2 »2H 2 0, along with sufficient watei- to bind the mixture.
- Aluminum oxide hydrates such as beta aluminum oxide monohydrate or alpha or beta alumina trihydrate may be substituted for boehmite, although not necessarily with equivalent results.
- acid chromium compounds may be substituted for Cr(OH)Cl 2 »2H 2 0, such as CrCl 3 , Cr(N0 3 ) 3 , Cr(OH) (CH j COO) ⁇ Cr(CH 3 COO) 3 , and Cr 3 (OH) 2 (CH 3 COO) 7 , although not necessarily with equivalent results.
- the acid chromium compounds are believed to peptize the aluminum oxide hydrate particles, resulting in a strong extrudate or pellet.
- the catalyst precursor may be prepared by extrusion, pelletizing or other methods of compacting the mixture.
- an extrudable dough is formed by mixing a finely divided boehmite powder, preferably about 10 to 75 microns in size, with Cr(OH)Cl 2 »2H 2 0 and water until a mixture suitable for extrusion results.
- a finely divided boehmite powder preferably about 10 to 75 microns in size
- Cr(OH)Cl 2 »2H 2 0 a finely divided boehmite powder
- Cr(OH)Cl 2 »2H 2 0 preferably about 10 to 75 microns in size
- Cr(OH)Cl 2 »2H 2 0 preferably about 10 to 75 microns in size
- Cr(OH)Cl 2 »2H 2 0 preferably about 10 to 75 microns in size
- Cr(OH)Cl 2 »2H 2 0 preferably about 10 to 75 microns in size
- Cr(OH)Cl 2 »2H 2 0
- Such extruded particles typically will have a diameter in the range of about 1.5 to 2 mm and have a length of about 1 to 3 times the diameter.
- the particles After being extruded the particles will be dried in air at temperatures in the range of about 20"C to 120*C, preferably 80*C to 100 * C, and then heated in nitrogen (not air) at about 300*C to 650'C, preferably 400'C to 550*C, for a suitable period of about 2 to 12 hours, preferably about 4 hours.
- the calcining operation serves to convert boehmite to A1 2 ° 3 and to convert Cr(OH)Cl 2 »2H,0 to surface amorphous Cr 2 0 3 .
- the calcined particles are then ready to be used in the fluorination of CFC-133a to HFC-134a. As will be seen below, heating the catalyst in nitrogen provides improved performance relative to heating the same catalyst in air.
- Fluorination of hydrocarbons and partially halogenated hydrocarbons may be carried out using the catalyst of the invention.
- Hydrogen atoms or halogen atoms are replaced by fluorine atoms by reaction with HF.
- HF fluorine atoms
- CFC-133a hydrogen fluoride
- HFC-134a 1,1,1,2- tetrafluoroethane
- halogenated hydrocarbons may be fluorinated with the catalyst of the invention, including such compounds as perchloroethylene (CC1 2 CC1 2 ) , partially chlorinated ethylenes, and chloro- and chlorofluoromethanes.
- perchloroethylene CC1 2 CC1 2
- partially chlorinated ethylenes ethylenes
- chloro- and chlorofluoromethanes chloro- and chlorofluoromethanes.
- 300*C to 450'C preferably about 325 ⁇ C to 400'C and at pressures in the range of 100 to 2,000 kPa, preferably about 172 to 517 kPa (gauge) .
- the mole ratio of HF/feed will be in the range of about 10/1 to 1/1, preferably 5/1 to 2/1.
- the liquid hourly space velocity for a fixed bed reactor will be about 0.5 to 5.0 hr "1 , preferably about
- HFC-134a in the feed is typically converted with a selectivity to HFC-134a of about 90 to 99%.
- Example 1 The catalyst prepared in Example 1 were tested by grinding the extrudates of Example 1 to 20-40 mesh size and then placing 30 mL of the particles in a 0.5 inch diameter i.d. (12.7 mm) reactor and then passing HF and CFC-133a (2.5/1 mol ratio) over the catalysts at a liquid hourly space velocity of 1.0 hr *1 (based on CFC- 133a) at a temperature of 350 * C and a pressure of 45 psig (310 kPa gauge) .
- the results showed the superiority of the extrudates which had been heated in nitrogen, as will be seen in Figures 1 and 2.
- the performance of the catalyst of the invention was equivalent to that of prior art catalysts consisting solely of Cr 2 0 3 and superior to the extrudate calcined in air instead of nitrogen with respect to both activity and selectivity. Since the catalyst of the invention is significantly less expensive than the conventional catalyst containing only chromium oxides, the catalyst of the invention provides an advantage to the user while retaining the performance of the conventional catalyst.
Abstract
An improved process for the vapor phase fluorination, especially fluorination of 1,1,1-trifluoro-2-chloroethane (CFC-133a) with HF to produce 1,1,1,2-tetrafluoroethane (HFC-134a) employs a catalyst which preferably consists essentially of boehmite and Cr(OH)Cl2.2H2O, combined and extruded to form particulates and then heated in nitrogen.
Description
PROCESS FOR THE MANUFACTURE OF 1.1.1.2-TETRAFLUOROETHANE
Fiel of the Ipverfcion This invention relates generally to the fluorination of halogenated hydrocarbons. More specifically, it relates to the fluorination with HF of l,l,l-trifluoro-2-chloroethane (CFC-133a) to produce 1,1,1,2-tetrafluoroethane (HFC-134a) , a compound likely to replace CFC-12 (dichlorodifluoromethane) in certain applications.
Prior Art CFC-12 is widely used in air conditioning equipment and other applications, but its use is being limited because of concern about depletion of the atmospheric ozone layer. One compound which may replace CFC-12 because it has much less potential for ozone depletion and has similar physical properties, is HFC- 134a (1,1,1,2-tetrafluoroethane) .
Many of the processes for preparing HFC-134a by reacting HF with CFC-133a employ catalysts entirely or partially composed of chromium oxides or fluorides.
In U.S. Pat. No. 3,258,500 fluorination with HF is carried out over an anhydrous chromium (III) oxide catalyst. In one aspect the catalyst is combined with alumina, although it is indicated that such supported catalysts are less effective.
In U.S. Pat. No. 4,158,675 a process is disclosed for producing HFC-134a by fluorination of CFC- 133a using a basic chromium fluoride catalyst. Two Japanese published applications, 55/027138 and 55/027139, also disclose vapor phase fluorination to produce HFC-134a using various Cr (III) compounds including chromium fluoride, oxides and oxyfluorides, which are pretreated under reaction conditions.
A catalyst prepared by co-depositing hexavalent chromium oxide and a transition metal compound on alumina and then fluorinating was suggested to be useful for the preparation of HFC-134a in U. S. Pat. No. 4,792,643. In EP 331991A HFC-134a is produced using a metal catalyst, preferably cobalt, supported on A1F3 or carbon.
Alumina is used as a support for a metal fluoride which may include chromium in O8910341-A. Chromium salts are impregnated on gamma-alumina in J02/157235A for a vapor phase reaction which produces CFC *-23 rather than HFC-134a.
A supported chromium oxide or halide is used to make HFC-134a in J02/172933A. Chromium is supported on A1F3 for preparation of HFC-134a in U.S. Pat. No. 4,766,260 and U.S. Pat. 5,008,475.
The possibility that HFC-134a will become a volume commercial product has caused renewed interest in improved processes to prepare it. The present invention particularly relates to a catalyst for such an improved process. In addition, the catalyst of the invention has application to other related fluorinations.
gumπary of the Invention
Vaporphase fluorination of hydrocarbons and/or halogenated hydrocarbons, and in particular fluorination of l,l,l-trifluoro-2-chloroethane (CFC-133a) to 1,1,1,2- tetrafluoroethane (HFC-134a) , may be carried out at fluorination conditions in the presence of HF over a catalyst produced by mixing an acidic chromium compound, preferably a chromium hydroxy chloride, Cr(OH)Cl2»2H20
with an aluminum oxide hydrate, preferably boehmite and water, then extruding pellets and heating in nitrogen (not air) .
In one embodiment the catalyst is prepared by mixing 95 to 9 wt.% of a finely powdered boehmite
(particles of about 10 to 75 microns) with 5 to 91 wt.% of Cr(OH)Cl2'2H20 and water to form a dough, which is then extruded to form particles suitable for use in a fixed bed reactor. The particles may be dried at a temperature of about 20"C to 120*C in air, preferably 70*C to 100βC, and thereafter, heated in nitrogen at 300*C to 650°C, preferably 400"C to 550*C, and held at the maximum temperature for about 2 to 12 hours, preferably about 4 hours. The process may be carried out in the vapor phase with a mole ratio of HF to CFC-133a of 10/1 to 1/1. Preferably, the mole ratio would be about 5/1 to 2/1. The reaction conditions include a temperature in the range of about 300*c to 450*C, preferably a temperature of about 325*C to 400*C, and a pressure in the range of 100 to 2,000 kPa, preferably about 172 to 517 kPa gauge. In a fixed bed reactor the liquid hourly space velocity will be about 0.5 to 5.0 hr* , preferably about 0.75 to 2 hr"1. based on the feedstock.
BRIEF DESCRIPTION OF THE DRAWINGS
Figures l and 2 show the activity and selectivity of catalysts of the invention in converting CFC-133a to HFC-134a.
Description of the Preferred Embodiments The Catalyst
The catalyst is made from an aluminum oxide hydrate, preferably boehmite (alpha alumina monohydrate i.e., AIO(OH) or A1203«H20) and an acidic chromium compound, preferably Cr(OH)Cl2»2H20 since the combination has been found to provide performance similar to the CF3 or Cr203 catalysts of the prior art, but at substantially lower cost. Preferably, the catalyst is the product resulting from calcining a mixture of about 95 to 9 wt.% boehmite and about 5 to 91 wt.% of Cr(OH)Cl2«2H20. Preferably, the mixture will contain about 90 to 65 wt.% boehmite and about ..■> to 10 wt.% of Cr(OH)Cl2»2H20, along with sufficient watei- to bind the mixture.
Other aluminum oxide hydrates such as beta aluminum oxide monohydrate or alpha or beta alumina trihydrate may be substituted for boehmite, although not necessarily with equivalent results.
Other acid chromium compounds may be substituted for Cr(OH)Cl2»2H20, such as CrCl3, Cr(N03)3, Cr(OH) (CHjCOO)^ Cr(CH3COO)3, and Cr3(OH)2(CH3COO)7, although not necessarily with equivalent results. The acid chromium compounds are believed to peptize the aluminum oxide hydrate particles, resulting in a strong extrudate or pellet.
The catalyst precursor may be prepared by extrusion, pelletizing or other methods of compacting the mixture. Preferably, an extrudable dough is formed by mixing a finely divided boehmite powder, preferably about 10 to 75 microns in size, with Cr(OH)Cl2»2H20 and water until a mixture suitable for extrusion results. Generally, such an extrudable dough must have suitable viscosity and stiffness. The dough may be extruded by various devices known in the art, such as an auger extruder or hydraulic piston extruder. This generally
requires pressures in the range of 35 to 6894 kPa in order to form extrudates suitable for use in a fixed bed reactor. Such extruded particles typically will have a diameter in the range of about 1.5 to 2 mm and have a length of about 1 to 3 times the diameter. After being extruded the particles will be dried in air at temperatures in the range of about 20"C to 120*C, preferably 80*C to 100*C, and then heated in nitrogen (not air) at about 300*C to 650'C, preferably 400'C to 550*C, for a suitable period of about 2 to 12 hours, preferably about 4 hours. The calcining operation serves to convert boehmite to A1 2°3 and to convert Cr(OH)Cl2»2H,0 to surface amorphous Cr203. The calcined particles are then ready to be used in the fluorination of CFC-133a to HFC-134a. As will be seen below, heating the catalyst in nitrogen provides improved performance relative to heating the same catalyst in air.
Fluorination Process Fluorination of hydrocarbons and partially halogenated hydrocarbons may be carried out using the catalyst of the invention. Hydrogen atoms or halogen atoms are replaced by fluorine atoms by reaction with HF. For example, when hydrogen fluoride is reacted with l,l,l,-trifluoro-2-chloroethane (CFC-133a) its chlorine atom is replaced with a fluorine atom, yielding 1,1,1,2- tetrafluoroethane (HFC-134a) . In addition to fluorination of CFC-133a, it is possible to fluorinate trichloroethylene to produce HFC-134a. Also, other halogenated hydrocarbons may be fluorinated with the catalyst of the invention, including such compounds as perchloroethylene (CC12CC12) , partially chlorinated ethylenes, and chloro- and chlorofluoromethanes.
Although the reaction itself is generally known, the yield of HFC-134a is affected by the catalyst used and the reaction conditions. Generally, as will be seen, the reaction will be carried out with the catalyst of the invention at temperatures in the range of about
300*C to 450'C, preferably about 325βC to 400'C and at pressures in the range of 100 to 2,000 kPa, preferably about 172 to 517 kPa (gauge) . The mole ratio of HF/feed will be in the range of about 10/1 to 1/1, preferably 5/1 to 2/1. The liquid hourly space velocity for a fixed bed reactor will be about 0.5 to 5.0 hr"1, preferably about
0.75 to 2 hr"1, based on the feedstock. Using the catalyst of the invention, about 10 to 30% of the CFC-
133a in the feed is typically converted with a selectivity to HFC-134a of about 90 to 99%.
It is desirable to pretreat the catalyst before introducing the feedstock, e.g. CFC-133a, by exposing the calcined catalyst to HF mixed with an inert gas (about 5 to 50 wt.%) at a temperature of about 325*C to 400*C for about 1 to 10 hours. Thereafter, feed can be introduced along with HF and some air (5 to 25 volume percent and the fluorination reaction initiated. The temperature will be adjusted to provide the desired conversion of the feed consistent with a high selectivity. Unreacted CFC- 133a is recovered from the effluent by distillation and recycled to the reactor. The product HFC-134a is separated from the by-products by distillation and purified as required for the expected end use.
A sample of 200 g of boehmite having 27.2% volatiles supplied by Kaiser Aluminum & Chemical Co. was mixed with 54.6 g of Cr(OH)Cl2»2H20 in a powder blender.
240 g of deionized water was added to the powder blend
and mixing was continued to form a dough, which was dried by indirect heating with steam until an extrudable consistency was reached. The dough was extruded to form 1/12 inch (2.12 mm) cylindrical extrudates. These extrudates were reduced to an average length/diameter ratio of 3/1. They were then dried in an oven at 90'C for 18 hours. After drying half of the extrudates were calcined in a muffle furnace at 500*C for 4 hours, while the other half was heated in nitrogen (to 300*C at 3βC/min and then to 500*C at l'C/min and held there for 4 hours) .
Example g
The catalyst prepared in Example 1 were tested by grinding the extrudates of Example 1 to 20-40 mesh size and then placing 30 mL of the particles in a 0.5 inch diameter i.d. (12.7 mm) reactor and then passing HF and CFC-133a (2.5/1 mol ratio) over the catalysts at a liquid hourly space velocity of 1.0 hr*1 (based on CFC- 133a) at a temperature of 350*C and a pressure of 45 psig (310 kPa gauge) . The results showed the superiority of the extrudates which had been heated in nitrogen, as will be seen in Figures 1 and 2. The performance of the catalyst of the invention was equivalent to that of prior art catalysts consisting solely of Cr203 and superior to the extrudate calcined in air instead of nitrogen with respect to both activity and selectivity. Since the catalyst of the invention is significantly less expensive than the conventional catalyst containing only chromium oxides, the catalyst of the invention provides an advantage to the user while retaining the performance of the conventional catalyst.
Claims
1. A process for the vapor phase fluorination of hydrocarbons and/or halogenated hydrocarbons with hydrogen fluoride over a catalyst at fluorination conditions wherein said catalyst consists essentially of the product of heating in nitrogen a mixture of an aluminum oxide hydrate and acidic chromium compound.
2. The process of Claim 1 wherein said catalyst consists essentially of the product of calcining a mixture of 95 to 9 wt.% boehmite and 5 to 91 Wt.% of Cr(0H)Cl2 «2H20.
3. The process of Claim 1 wherein 1,1,1- trifluoro-2-chloroethane (CFC-133a) is fluorinated to 1,1,1,2-tetrafluoroethane (HFC-134a) .
4. A process for preparing a fluorination catalyst comprising:
(a) mixing powdered aluminum oxide hydrate with an acidic chromium compound and water to form an extrudable dough;
(b) extruding said dough to form particles suitable for use in fixed bed reactors;
(c) drying said particles in air at temperatures in the range of about 20°C to 120βC, (d) heating the dried particles of (c) in nitrogen at temperatures in the range of about 300°C to
650°c,
(e) recovering the catalyst after calcining of (d) .
5. The process of Claim 4 wherein said aqueous solution contains 5 to 6 wt.% Cr(0H)Cl2*2H20.
6. The process of Claim 4 wherein said aluminum oxide hydrate is boehmite having a mean particle size of about 10 to 75 microns.
7. The process of Claim 4 wherein said heating of (d) is carried out at about 300°C to 650°C for about 2 to 12 hours.
8. The process of Claim 4 further comprising the step (f) of pretreating the finished catalyst of (c) with HF in an inert gas at a temperature of about 325°C to 400°C for about 1 to 10 hours.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US78292891A | 1991-10-25 | 1991-10-25 | |
US782,928 | 1991-10-25 |
Publications (1)
Publication Number | Publication Date |
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WO1993008146A1 true WO1993008146A1 (en) | 1993-04-29 |
Family
ID=25127618
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/US1992/008924 WO1993008146A1 (en) | 1991-10-25 | 1992-10-19 | Process for the manufacture of 1,1,1,2-tetrafluoroethane |
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AU (1) | AU2892292A (en) |
WO (1) | WO1993008146A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001017676A1 (en) * | 1999-09-09 | 2001-03-15 | Basell Polyolefine Gmbh | Method for producing phillips catalysts for polymerising olefins with better productivity rates in the particle-form process |
US9771309B2 (en) | 2005-04-08 | 2017-09-26 | Mexichem Amanco Holding S.A. De C.V. | Chromia based fluorination catalyst |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2252126A1 (en) * | 1973-11-22 | 1975-06-20 | Instititul Central Cercetari C | Chrome-alumina extruded catalysts - of increased strength by impregnating mixed easily and difficultly peptized alumina particles with aq. chromic acid |
EP0417680A1 (en) * | 1989-09-13 | 1991-03-20 | Hoechst Aktiengesellschaft | Method for the production of 1,1,1,2-tetrafluoroethane |
US5155082A (en) * | 1991-04-12 | 1992-10-13 | Allied-Signal Inc. | Catalyst for the manufacture of chlorofluorocarbons, hydrochlorofluorocarbons and hydrofluorocarbons |
EP0408005B1 (en) * | 1989-07-12 | 1994-03-02 | AUSIMONT S.p.A. | Process for preparing 1,1,1,2-tetrafluoroethane |
-
1992
- 1992-10-19 AU AU28922/92A patent/AU2892292A/en not_active Abandoned
- 1992-10-19 WO PCT/US1992/008924 patent/WO1993008146A1/en active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2252126A1 (en) * | 1973-11-22 | 1975-06-20 | Instititul Central Cercetari C | Chrome-alumina extruded catalysts - of increased strength by impregnating mixed easily and difficultly peptized alumina particles with aq. chromic acid |
EP0408005B1 (en) * | 1989-07-12 | 1994-03-02 | AUSIMONT S.p.A. | Process for preparing 1,1,1,2-tetrafluoroethane |
EP0417680A1 (en) * | 1989-09-13 | 1991-03-20 | Hoechst Aktiengesellschaft | Method for the production of 1,1,1,2-tetrafluoroethane |
US5155082A (en) * | 1991-04-12 | 1992-10-13 | Allied-Signal Inc. | Catalyst for the manufacture of chlorofluorocarbons, hydrochlorofluorocarbons and hydrofluorocarbons |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001017676A1 (en) * | 1999-09-09 | 2001-03-15 | Basell Polyolefine Gmbh | Method for producing phillips catalysts for polymerising olefins with better productivity rates in the particle-form process |
US6699947B1 (en) | 1999-09-09 | 2004-03-02 | Basell Polyolefine Gmbh | Method for producing Phillips catalysts for polymerizing olefins with better productivity rates in the particle-form process |
US9771309B2 (en) | 2005-04-08 | 2017-09-26 | Mexichem Amanco Holding S.A. De C.V. | Chromia based fluorination catalyst |
US10189757B2 (en) | 2005-04-08 | 2019-01-29 | Mexichem Amanco Holding S.A. De C.V. | Chromia based fluorination catalyst |
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Publication number | Publication date |
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AU2892292A (en) | 1993-05-21 |
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