WO1992018447A1 - Process for producing hydrochloromethanes - Google Patents
Process for producing hydrochloromethanes Download PDFInfo
- Publication number
- WO1992018447A1 WO1992018447A1 PCT/JP1992/000522 JP9200522W WO9218447A1 WO 1992018447 A1 WO1992018447 A1 WO 1992018447A1 JP 9200522 W JP9200522 W JP 9200522W WO 9218447 A1 WO9218447 A1 WO 9218447A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- reaction
- reduction
- selectivity
- carbon tetrachloride
- Prior art date
Links
Classifications
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/462—Ruthenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/72—Copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8926—Copper and noble metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
- C07C19/03—Chloromethanes
- C07C19/04—Chloroform
Definitions
- the present invention uses polychloromethanes, particularly tetrachloromethane carbon, which is regulated from the standpoint of protecting the global environment, as a raw material, and uses this as a raw material for various fluorine-based compounds, such as hydrogen-containing porcelain such as porcine form. It relates to a method for converting to chloromethanes.
- carbon tetrachloride has been mainly used as a raw material for various types of fluorocarbons, but the production of carbon tetrachloride as a raw material as well as these fluorocarbons has been regulated. Or technology to convert to useful ones is widely demanded worldwide.
- the present inventors have studied variously the above-mentioned gas-phase hydrogen reduction method. First, analysis of the organic components on the deactivated catalyst revealed that most of them were polymers. The catalyst particle size was almost the same as when the catalyst was not used, based on observation by transmission electron microscope and analysis by X-ray diffraction. Therefore, it is estimated that polymer accumulation is the main cause of deactivation. -Yes.
- the present inventors have intensively studied a reaction method for suppressing rapid deactivation of a catalyst. As a result, short-term deterioration of the catalyst can be eliminated and hydrogen-containing chloromethanes can be obtained in high yield by adopting the method of reducing borochloromethanes in the liquid phase with hydrogen in the presence of a reduction catalyst.
- the present invention has been completed on the basis of the above-mentioned findings, and is a method for producing hydrogen-containing chlorinated hydrogens, comprising reducing polychloromethanes with hydrogen in a liquid phase in the presence of a reduction catalyst. It provides Hereinafter, details of the present invention will be described with examples.
- Polychloromethanes are carbon tetrachloride, chloroform, and methylene chloride. According to the method of the present invention, the reduction of carbon tetrachloride forms carbon, methylene chloride, and methyl chloride, the reduction of methylene chloride and methyl chloride, and the reduction of methylene chloride by reduction of methylene chloride. Methyl is obtained. As polychloromethanes, regulated carbon tetrachloride is preferable.
- Carbon tetrachloride is a molecule in which four highly polar chlorine atoms are bonded to carbon atoms, and has extremely high adsorption energy among halogenated methanes. Therefore, the residence time on the catalyst is long, and it is easily catalyzed. Therefore, when a catalyst composed of elements with high reduction activity selected from groups 8, 9 and 10 is used, the formation of olefins and the formation of polymers are remarkable, and they tend to be deactivated in a very short time. . Particularly, in the gas phase reaction method, since basically the reaction temperature strength s high, likely to occur generation Polymerization of Orefin acids, also since the resulting polymer generally having a high boiling point, difficult to remove from the catalyst surface It is possible. This is thought to be the cause of the rapid deactivation.
- the reduction catalyst at least one element selected from the group 8 elements of iron, ruthenium, and osmium, the group 9 elements of conolite, rhodium, and iridium, and the group 10 elements of nickel, palladium, and platinum are used. Catalysts based on the main component are preferred.
- the catalyst mainly composed of the group 8, 9 or 10 element may be a catalyst composed of only these elements, and a metal element other than the group 8 to 10 element is further added to these elements. A catalyst used in combination may be used.
- platinum group elements such as palladium, ruthenium, platinum, and platinum oxide are particularly preferable because of high activity and high durability.
- additional component include Group 11 elements such as copper, silver, and gold. Both the main component element and the additional component element may be used alone or in combination of two or more. When an additive is used in combination, the amount is preferably 0.01 to 50% by weight, more preferably 0.1 to 50% by weight, and particularly preferably 1 to 50% by weight.
- catalyst metals can be used as they are, or those supported on a carrier.
- the carrier those usually used, such as activated carbon, alumina, zirconia, and silica, can be used.
- the loading amount is preferably about 0.01 to 20% by weight, more preferably about 0.5 to 5% by weight, from the viewpoints of catalyst loading efficiency, reaction activity and dispersion of catalyst components.
- the method for supporting the catalyst component and the like can also be appropriately selected from the range usually employed. For example, a method in which a simple salt or a complex salt of the above-mentioned element is used and supported by an impregnation method, an ion exchange method, or the like can be applied. Also, the catalyst when the use of, but not necessarily need to perform the reduction treatment of the catalyst, desirable for obtaining a force 3 stabilization characteristics that preliminarily subjected to a hydrogen reduction. As a method for reducing the supported catalyst component, a method of reducing in a liquid phase with hydrogen, hydrazine, formaldehyde, sodium borohydride, or the like, and a method of reducing in a gas phase with hydrogen can be applied.
- any of a fixed bed and a suspension bed can be adopted.
- the use of a reaction solvent is effective for controlling the product ratio, stabilizing the reaction activity, and the like, and can be performed as appropriate.
- alcohols such as methanol and ethanol
- amines such as triethylamine
- carboxylic acids such as acetic acid
- ketones such as acetone
- liquid phase reduction reaction in the present invention When the liquid phase reduction reaction in the present invention is performed continuously, it is preferable to employ a liquid phase fixed bed system in which a raw material solution is brought into contact with a fixed bed of a reduction catalyst.
- a liquid phase fixed bed system in which a raw material solution is brought into contact with a fixed bed of a reduction catalyst.
- the liquid phase diffusion distance of hydrogen is short, and it is easy to suppress a decrease in the hydrogen concentration on the catalyst surface.
- the carrier a carrier having such a strength as not to be powdered by the flow of the liquid is employed.
- the shape of the carrier is preferably in the form of pellets, which are hardly subject to abrasion loss, particularly when the raw material liquid is circulated in the upflow.
- crushed charcoal or the like can be used, and is not necessarily limited.
- the size of the catalyst is also not particularly limited, but usually, a catalyst having a diameter of about 0.5 to 210111111 is appropriate.
- the temperature of the liquid phase reduction reaction is 0 "C to 200 ° C, preferably 50 to 150'C.
- the reaction molar ratio between hydrogen and polychloromethane is not particularly limited. Increasing the amount of hydrogen increases the reaction rate, but increases the rate of dechlorination and hydrogenation, but increases the rate of production Use about 0.1 to 10 moles of hydrogen per mole of polychloromethane It is possible to increase the efficiency of hydrogen utilization by recycling excess hydrogen.
- reaction pressure is suitably normal pressure or higher, and the reaction speed increases as the pressure increases. Pressurization up to several kg / cm 2 'G to about 10 kg / cm 2 ' G can be employed. At too high a pressure, difficulties such as an increase in equipment costs are observed even if the reaction rate increases.
- the reaction was continued by supplying the mixture continuously in moles.
- the reaction rate of carbon tetrachloride at 1,000 hours after the start of the reaction was 91%, and formation of chloroform (selectivity: 70%), perchloroethylene (selectivity: 18%), etc. was confirmed.
- One liter of carbon tetrachloride was put into an autoclave having an internal volume of 2 liters, and 50 g of an alumina-supported palladium catalyst (supporting amount: 2% by weight, manufactured by Nichi-Kemkyat Co.) was added. After charging nitrogen, the temperature was raised to 115 eC, and then the supply of hydrogen was started. The pressure was 5 kgZcm 2 'G. For the product, the gas phase component, the liquid phase component, and the phase difference were also analyzed using gas chromatography. The reaction was continued by continuously supplying 4 mol of hydrogen to 1 mol of carbon tetrachloride.
- the reaction rate of carbon tetrachloride at 1,000 hours after the start of the reaction is 92%, such as chloroform (selectivity: 60%), methylene chloride (selectivity: 9%), perchlorethylene (selectivity: 17%), etc. Generation was confirmed.
- the reaction was continued by supplying 5 units of nitrogen continuously.
- the reaction rate of carbon tetrachloride at 1,000 hours after the start of the reaction was 89%, and the form of chloroform (selectivity: 58%), methylene chloride (selectivity: 9%), and methyl chloride (selectivity: 1) 4%) and perchlorethylene (selectivity: 18%).
- Activated carbon-supported platinum catalyst (supporting amount: 0.5% by weight: manufactured by Nichi-Im Chemical Co., Ltd.) 100 ⁇ was placed in a 0.5 inch inner diameter Inconel reaction tube, and the heat was set to 160. It was immersed in the medium. After preliminarily treating with nitrogen and then with hydrogen, hydrogen was introduced at a ratio of 2 mol per mol of carbon tetrachloride, and the reaction was carried out in the gas phase. The contact time was 7 seconds and the reaction pressure was normal pressure. The reaction rates of carbon tetrachloride at 2 hours and 20 hours after the start of the reaction were about 90% and about 30%, respectively, and were deactivated over time thereafter. As the products, chlorinated alkanes and alkenes having 2 to 5 carbon atoms, such as perchloroethylene, were recognized in addition to black form, salted methylene, methyl chloride, and methane.
- acetylene black powder 100 g of acetylene black powder (average particle size: 1 m) as a carrier was put into 1 liter of ion-exchanged water.
- Rhodium chloride and chloroauric acid were dissolved in ion-exchanged water in a weight ratio of metal components of 95: 5, respectively, in an amount corresponding to 2% of the weight of the carrier.
- the mixture was washed with ion-exchanged water and dried at 110 eC .
- pitch-based activated carbon powder 100 g of pitch-based activated carbon powder (average particle size of 10 to 20 ⁇ ) as a carrier was charged into one liter of ion-exchanged water.
- Nickel chloride, chloroplatinic acid, and chloroauric acid were dissolved in ion-exchanged water at a weight ratio of metal components of 5: 4: 1, respectively, in an amount corresponding to 2% of the weight of the carrier.
- After reduction with an aqueous solution of sodium borohydride it was washed with ion-exchanged water and dried at 110.
- the solution was made alkaline with the addition of water, and then reduced with an aqueous solution of hydrazine. After washing with ion-exchanged water, it was dried at 110.
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was set to 110 using the reduction catalyst according to Preparation Example 2.
- the reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 78%, and the form of chloroform (selectivity: 85%), hexacloane (selectivity: 5%), methylene chloride (selectivity: 8%) ) Etc. were confirmed.
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was set to 100 using the reduction catalyst according to Preparation Example 3.
- the reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 85%, and the form of chloroform (selectivity: 90%), hexacloane (selectivity: 5%), and pentachloroethane (selectivity: 2%) ), Tetrachloroethylene (selectivity: 2%), etc. were confirmed.
- Example 1 2 The reaction was carried out in the same manner as in Example 8, except that the reduction catalyst according to Preparation Example 4 was used. After 100 hours from the start of the reaction, the conversion rate of carbon tetracarbonate was 86%, and formation of chloroform (selectivity: 92%), hexanechloroethane (selectivity: 4%), and the like was confirmed.
- Example 1 2 the reduction catalyst according to Preparation Example 4 was used. After 100 hours from the start of the reaction, the conversion rate of carbon tetracarbonate was 86%, and formation of chloroform (selectivity: 92%), hexanechloroethane (selectivity: 4%), and the like was confirmed.
- Example 1 2 The reaction was carried out in the same manner as in Example 8, except that the reduction catalyst according to Preparation Example 4 was used. After 100 hours from the start of the reaction, the conversion rate of carbon tetracarbonate was 86%, and formation of chloroform (selectivity: 92%)
- the reaction was carried out in the same manner as in Example 8 except that the reaction temperature was set to 100 using the reduction catalyst according to Preparation Example 5.
- the reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 84%.
- the formation of black mouth form (selectivity: 89%), hexachloroethane (selectivity: 6%), etc. was confirmed.
- Example 14 The reaction was carried out in the same manner as in Example 8, except that the reduction catalyst according to Preparation Example 6 was used.
- the reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 90%, and formation of chloroform (selectivity: 92%), hexanechloroethane (selectivity: 3%), and the like was confirmed.
- Example 14 The reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 90%, and formation of chloroform (selectivity: 92%), hexanechloroethane (selectivity: 3%), and the like was confirmed.
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was set to 110 ° C using the reduction catalyst according to Preparation Example 7. 100 hours after the start of the reaction, the reaction rate of carbon tetrachloride is 75%, and the formation of chloroform (selectivity: 85%), hexachloroethane (selectivity: 6%), methylene chloride (selectivity: 7%), etc. was confirmed.
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was set to 100 eC using the reduction catalyst according to Preparation Example 8. 100 hours after the start of the reaction, the reaction rate of carbon tetrachloride was 71%, and the form of chloroform (selectivity: 90%), hexachloroethane (selectivity: 4%), and phenol (selectivity: 2) %) And tetrachloroethylene (selectivity: 2%).
- Example 17 The reaction was carried out in the same manner as in Example 8, except that the reduction catalyst according to Preparation Example 9 was used. 100 hours after the start of the reaction, the tetrachlorocarbon reaction rate was 84%, and formation of chloroform (selectivity: 97%), tetrachloroethane (selectivity: 3%), etc. was confirmed. Was.
- Example 17 The reduction catalyst according to Preparation Example 9 was used. 100 hours after the start of the reaction, the tetrachlorocarbon reaction rate was 84%, and formation of chloroform (selectivity: 97%), tetrachloroethane (selectivity: 3%), etc. was confirmed. Was.
- Example 17 Example 17
- the reaction was carried out in the same manner as in Example 8 except that the reduction catalyst according to Preparation Example 10 was used. 100 hours after the start of the reaction, the conversion of carbon tetrachloride is 83%, and the form of chloroform (selectivity: 69%), hexachloroethane (selectivity: 28%), methylene chloride (selectivity: 1%), tetrachloroethylene (Selectivity: 2%).
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was set to 120 ° C. using the reduction catalyst according to Preparation Example 11.
- the reaction rate of carbon tetrachloride at 100 hours after the start of the reaction was 84%. - ⁇ ⁇ -Yes, formation of black mouth form (selectivity: 87%), hexachlorene (selectivity: 6%), methylene chloride (selectivity: 7%), etc. was confirmed.
- the reaction was carried out in the same manner as in Example 8, except that the reaction temperature was 90 using the reduction catalyst according to Preparation Example 12. After 100 hours from the start of the reaction, the conversion rate of tetrachlorosilane is 74%, and the form of chloroform is (selectivity: 89%), hexachloroethane (selectivity: 5%), and pentachloroethane (selectivity: 2%). , Tetrachloroethylene (selectivity: 3%), etc. were confirmed.
- the reaction was carried out in the same manner as in Example 8 except that the reduction catalyst according to Preparation Example 13 was used.
- the reaction rate of carbon tetrachloride 100 hours after the start of the reaction was 87%, and formation of chloroform (selectivity: 93%), hexachloroethane (selectivity: Wo) and the like was confirmed.
- the present invention as shown in the examples, has the effect of producing high-yield hydrogen-containing chloromethanes such as chloroform by reducing polychloromethanes, particularly carbon tetrachloride with hydrogen in the liquid phase. Having.
- the method of the present invention has an effect that even if the reaction rate of the raw material polychloromethans is increased, the hydrogen chloromethanes such as the desired product, such as chloroform, can be obtained with a high selectivity. Furthermore, the method of the present invention is extremely advantageous also from the viewpoint of catalyst life, because a side reaction that generates impurities that impair the catalytic activity can be effectively suppressed.
Landscapes
- 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)
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US07/960,423 US5334782A (en) | 1991-04-23 | 1991-04-23 | Method for producing a hydrogen-containing chloromethane |
EP92909542A EP0536420B1 (en) | 1991-04-23 | 1992-04-23 | Process for producing hydrochloromethanes |
DE69216977T DE69216977T2 (de) | 1991-04-23 | 1992-04-23 | Verfahren zur herstellung von hydrochlormethanen |
KR1019920703206A KR100222459B1 (ko) | 1991-04-23 | 1992-04-23 | 함수소 클로로메탄류의 제조방법 |
CA002086110A CA2086110C (en) | 1991-04-23 | 1992-04-23 | Method for producing hydrochloromethanes |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP3/119457 | 1991-04-23 | ||
JP3119457A JPH04327546A (ja) | 1991-04-23 | 1991-04-23 | 含水素クロロメタン類の製造法 |
JP3/352257 | 1991-12-13 | ||
JP3352257A JP3004115B2 (ja) | 1991-12-13 | 1991-12-13 | 含水素クロロアルカン類の製法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1992018447A1 true WO1992018447A1 (en) | 1992-10-29 |
Family
ID=26457193
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1992/000522 WO1992018447A1 (en) | 1991-04-23 | 1992-04-23 | Process for producing hydrochloromethanes |
Country Status (6)
Country | Link |
---|---|
US (1) | US5334782A (ja) |
EP (1) | EP0536420B1 (ja) |
KR (1) | KR100222459B1 (ja) |
CA (1) | CA2086110C (ja) |
DE (1) | DE69216977T2 (ja) |
WO (1) | WO1992018447A1 (ja) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994022792A1 (en) * | 1993-03-26 | 1994-10-13 | British Technology Group Limited | Catalytic method of replacing halogen in halocarbons |
US5476984A (en) * | 1994-04-14 | 1995-12-19 | The Dow Chemical Company | Hydrodechlorination process and catalyst for use therein |
US5817896A (en) * | 1993-03-26 | 1998-10-06 | The University Court Of The University Of Dundee | Catalytic method of replacing halogen in halocarbons |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5621151A (en) * | 1990-10-09 | 1997-04-15 | E. I. Du Pont De Nemours And Company | Halocarbon hydrogenolysis |
GB0020910D0 (en) * | 2000-08-25 | 2000-10-11 | Univ Birmingham | Reduction method |
IT1319258B1 (it) * | 2000-10-31 | 2003-09-26 | Sued Chemie Mt Srl | Catalizzatore per la idrodeclorurazione del tetracloruro di carbonio acloroformio. |
KR100484508B1 (ko) * | 2002-09-27 | 2005-04-20 | 학교법인 포항공과대학교 | 사염화탄소 처리방법 |
CN102690203A (zh) * | 2011-03-22 | 2012-09-26 | 中国科学院大连化学物理研究所 | 一种制备1,3-环己二甲胺的方法 |
TWI537347B (zh) * | 2015-04-02 | 2016-06-11 | 綠點高新科技股份有限公司 | 用於催化性油墨的芯鞘型催化劑 |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH021414A (ja) * | 1988-03-28 | 1990-01-05 | Kanto Denka Kogyo Co Ltd | ハロゲン化炭素又はハロゲン化炭化水素中のハロゲンを水素に置換する方法 |
JPH03133939A (ja) * | 1989-10-20 | 1991-06-07 | Asahi Glass Co Ltd | 部分塩素化メタンの製造方法 |
EP0455547A1 (fr) * | 1990-05-03 | 1991-11-06 | Elf Atochem S.A. | Procédé de déchloration des chlorométhanes supÀ©rieurs |
EP0460138A1 (en) * | 1989-12-22 | 1991-12-11 | Ercros S.A. | Method for producing chloroform |
JPH0426636A (ja) * | 1990-05-22 | 1992-01-29 | Asahi Glass Co Ltd | ハロゲン化炭素の還元方法 |
EP0479116A1 (en) * | 1990-10-04 | 1992-04-08 | The Dow Chemical Company | Vapor phase hydrogenation of carbon tetrachloride |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3579596A (en) * | 1968-03-29 | 1971-05-18 | Dow Chemical Co | Hydrogenolysis of carbon tetrachloride and chloroform |
BE1004608A3 (fr) * | 1990-11-16 | 1992-12-22 | Solvay | Procede pour la fabrication du chloroforme a partir de tetrachlorure de carbone, compositions catalytiques et procede pour leur obtention. |
-
1991
- 1991-04-23 US US07/960,423 patent/US5334782A/en not_active Expired - Lifetime
-
1992
- 1992-04-23 WO PCT/JP1992/000522 patent/WO1992018447A1/ja active IP Right Grant
- 1992-04-23 EP EP92909542A patent/EP0536420B1/en not_active Expired - Lifetime
- 1992-04-23 CA CA002086110A patent/CA2086110C/en not_active Expired - Lifetime
- 1992-04-23 DE DE69216977T patent/DE69216977T2/de not_active Expired - Lifetime
- 1992-04-23 KR KR1019920703206A patent/KR100222459B1/ko not_active IP Right Cessation
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH021414A (ja) * | 1988-03-28 | 1990-01-05 | Kanto Denka Kogyo Co Ltd | ハロゲン化炭素又はハロゲン化炭化水素中のハロゲンを水素に置換する方法 |
JPH03133939A (ja) * | 1989-10-20 | 1991-06-07 | Asahi Glass Co Ltd | 部分塩素化メタンの製造方法 |
EP0460138A1 (en) * | 1989-12-22 | 1991-12-11 | Ercros S.A. | Method for producing chloroform |
EP0455547A1 (fr) * | 1990-05-03 | 1991-11-06 | Elf Atochem S.A. | Procédé de déchloration des chlorométhanes supÀ©rieurs |
JPH0426636A (ja) * | 1990-05-22 | 1992-01-29 | Asahi Glass Co Ltd | ハロゲン化炭素の還元方法 |
EP0479116A1 (en) * | 1990-10-04 | 1992-04-08 | The Dow Chemical Company | Vapor phase hydrogenation of carbon tetrachloride |
Non-Patent Citations (1)
Title |
---|
See also references of EP0536420A4 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994022792A1 (en) * | 1993-03-26 | 1994-10-13 | British Technology Group Limited | Catalytic method of replacing halogen in halocarbons |
US5817896A (en) * | 1993-03-26 | 1998-10-06 | The University Court Of The University Of Dundee | Catalytic method of replacing halogen in halocarbons |
US5476984A (en) * | 1994-04-14 | 1995-12-19 | The Dow Chemical Company | Hydrodechlorination process and catalyst for use therein |
Also Published As
Publication number | Publication date |
---|---|
CA2086110C (en) | 1999-05-11 |
US5334782A (en) | 1994-08-02 |
EP0536420A4 (en) | 1993-09-29 |
DE69216977T2 (de) | 1997-05-15 |
EP0536420B1 (en) | 1997-01-22 |
CA2086110A1 (en) | 1992-10-24 |
DE69216977D1 (de) | 1997-03-06 |
EP0536420A1 (en) | 1993-04-14 |
KR100222459B1 (ko) | 1999-10-01 |
KR930701369A (ko) | 1993-06-11 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP2209759B1 (en) | Manufacture of 1,1,1,2,3,3-hexafluoropropane and 1,1,1,2-tetrafluoropropane via catalytic hydrogenation | |
JP4958790B2 (ja) | ハイドロフルオロアルカノールのハイドロフルオロアルケンへの接触転化 | |
EP2457889B1 (en) | Process for production of 2-chloro-3,3,3-trifluoropropene | |
EP2473275B1 (en) | Catalysts for fluoroolefins hydrogenation | |
JP6827810B2 (ja) | ハイドロフルオロオレフィンの製造方法 | |
JP6673413B2 (ja) | フルオロオレフィンの製造方法 | |
US7179440B2 (en) | Process to obtain hydrogen peroxide | |
WO2016031778A1 (ja) | ハイドロフルオロオレフィンの製造方法 | |
WO1992018447A1 (en) | Process for producing hydrochloromethanes | |
CN102762523B (zh) | 3,3,3-三氟丙烯的制造方法 | |
JPH08239336A (ja) | 金属による触媒作用の下でのパーフルオルアルキルアイオダイドテロマーの製造方法 | |
JPH04321634A (ja) | 1,1,2−トリクロロ−1,2,2−トリフルオロエタンを出発物質としてクロロトリフルオロエチレン及びトリフルオロエチレンを調製する方法及びこの方法に用いられる触媒組成物 | |
CN113634275B (zh) | 一种催化加氢脱氯用催化剂及其制备方法和应用 | |
US6291729B1 (en) | Halofluorocarbon hydrogenolysis | |
CN111013604A (zh) | 一种催化加氢脱氯用催化剂及其制备方法和应用 | |
JP3031508B2 (ja) | 多塩素化アルカン類の還元方法 | |
US8940948B2 (en) | Process for the manufacture of fluorinated olefins | |
WO2018123911A1 (ja) | 含塩素プロペンの製造方法 | |
CN113649030B (zh) | 加氢脱卤催化剂和三氟氯乙烯与三氟乙烯的制备方法 | |
JP5400148B2 (ja) | ヘキサフルオロイソプロパノールを生成する連続方法 | |
CN104692998B (zh) | 1,1-二氟-2-氯乙烷的制备方法 | |
JP3004115B2 (ja) | 含水素クロロアルカン類の製法 | |
JPH04327546A (ja) | 含水素クロロメタン類の製造法 | |
JPH0517379A (ja) | 含水素クロロフルオロカーボン類または含水素フルオロカーボン類の製法 | |
CN114605224A (zh) | 一种1,1,2,2,3,3,4-七氟环戊烷及其制备方法和应用 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): CA KR US |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FR GB GR IT LU MC NL SE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1019920703206 Country of ref document: KR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2086110 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1992909542 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 1992909542 Country of ref document: EP |
|
WWG | Wipo information: grant in national office |
Ref document number: 1992909542 Country of ref document: EP |