WO1995017366A1 - Procede de purification de 1,1,1,3,3-pentafluoro-2,3-dichloropropane - Google Patents
Procede de purification de 1,1,1,3,3-pentafluoro-2,3-dichloropropane Download PDFInfo
- Publication number
- WO1995017366A1 WO1995017366A1 PCT/JP1994/002161 JP9402161W WO9517366A1 WO 1995017366 A1 WO1995017366 A1 WO 1995017366A1 JP 9402161 W JP9402161 W JP 9402161W WO 9517366 A1 WO9517366 A1 WO 9517366A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- dichloropropane
- pentafluoro
- azeotropic composition
- hydrogen fluoride
- mixture
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 14
- XAHBEACGJQDUPF-UHFFFAOYSA-N 1,2-dichloro-1,1,3,3,3-pentafluoropropane Chemical compound FC(F)(F)C(Cl)C(F)(F)Cl XAHBEACGJQDUPF-UHFFFAOYSA-N 0.000 title claims abstract 9
- 239000000203 mixture Substances 0.000 claims abstract description 75
- 239000007791 liquid phase Substances 0.000 claims abstract description 28
- 238000004821 distillation Methods 0.000 claims abstract description 25
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000009835 boiling Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 2
- 235000008429 bread Nutrition 0.000 claims 1
- 239000007788 liquid Substances 0.000 abstract description 17
- 238000010533 azeotropic distillation Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 4
- 238000005259 measurement Methods 0.000 description 4
- 229910052787 antimony Inorganic materials 0.000 description 3
- -1 antimony halide Chemical class 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 229910002056 binary alloy Inorganic materials 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 238000001577 simple distillation Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000000998 batch distillation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000008280 chlorinated hydrocarbons Chemical class 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000004868 gas analysis Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/19—Fluorine; Hydrogen fluoride
- C01B7/191—Hydrogen fluoride
- C01B7/195—Separation; Purification
- C01B7/196—Separation; Purification by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/08—Acyclic saturated compounds containing halogen atoms containing fluorine
- C07C19/10—Acyclic saturated compounds containing halogen atoms containing fluorine and chlorine
Definitions
- the present invention provides a method for separating HF from a mixture mainly comprising hydrogen fluoride (hereinafter referred to as HF) and 1,1, 1.3.3 monopentafluoro-2.3-dichlorobutapan (hereinafter referred to as R-225 da). , R-225 da, enrichment or purification, and R-225 da separation from such a mixture to concentrate or purify HF.
- HF hydrogen fluoride
- R-225 da 1,1, 1.3.3 monopentafluoro-2.3-dichlorobutapan
- R-225 da is usually produced by reacting HF with a chlorinated hydrocarbon such as hexaclopropene in the presence of, for example, an antimony halide.
- the method for separating R-225 da from the reaction mixture formed in this case is generally a mixture comprising HF and R-225 da obtained by removing the catalyst by simple distillation of the reaction mixture. Washing with water to separate R—225 da.
- a large amount of dilute hydrofluoric acid aqueous solution is generated, and equipment for treating these is required.
- the above-mentioned separation method is not always effective because a large amount of water is required to neutralize the solution.
- the present inventors have conducted research on a method for separating HF from a mixture mainly composed of HF (boiling point at 1 atm: 20 ° C) and R-22 ⁇ da (boiling point at 1 atm: 50.4 ° C). As a result, it was found that HF and R-225 da formed a minimum azeotropic composition of about 90 10 (molar ratio) (boiling point 18 ° C, 1 Xg / cra 2 (abs.)).
- azeotropic compositions are enriched in HF-rich upper liquid phase (liquid phase) and R- 225 da at temperatures commonly used in industry, such as 80-160 ° C.
- the present invention has been completed by finding that it separates (ie, separates) into a lower liquid phase (liquid layer).
- the present invention provides an azeotropic composition consisting essentially of HF and R-225 da, and more particularly comprises 85-95 moles of HF at a pressure of 1-5 kg g cn! 2 (abs.).
- An azeotropic composition (boiling point: 18 to 50 ° C) containing 15 to 5 mol% of R-225da.
- the present invention utilizes the formation of the azeotropic composition described above to distill a mixture comprising HF and R-225 da to form HF and R-225 da together.
- a method for separating HF and R-225 da from a mixture characterized in that the mixture is distilled as a boiling composition and the residue is obtained as a bottom product.
- the residue is preferably rich in one component, more preferably substantially Consists of only one component.
- a mixture as a feedstock comprising HF and R-225 da is subjected to an azeotropic distillation step, and an azeotropic composition is distilled from a concentration section of the distillation step, for example, from the top of the column.
- the content of HF is reduced from that of the feedstock, preferably R-225da, which is substantially free of HF, or R-225da.
- HF having a lower content of HF than that of the feedstock, preferably substantially free of R-225 da is obtained from the recovery part of the distillation step, for example the bottom of the column.
- a method for separating (or purifying) R-225da or HF by separating R-225da is provided.
- an azeotropic mixture substantially consisting of HF and R-225 da distilled by azeotropic distillation is converted into an HF-rich upper liquid phase and R- Separate into the lower liquid phase rich in 2 25 da, supply the lower liquid phase to another distillation column, subject it to azeotropic distillation again to distill the azeotropic composition from the top of the column, and remove HF
- the present invention provides a method for separating HF and enriching R-225 da, which comprises obtaining R-225 da substantially free from the bottom of the column.
- the separated upper liquid phase is subjected to azeotropic distillation to distill the azeotropic composition from the top of the column to obtain HF containing substantially no R-225 da from the bottom of the column. It provides a method to separate 25 da and concentrate HF.
- composition of the feedstock refers to This means that it is inevitably determined based on the result of comparing the composition of HF and R-225 da in the mixture as the feedstock with the azeotropic composition.
- a mixture comprising 225 da as a main component, preferably R-225 da substantially free of HF, means that it can be obtained from the recovery part of the distillation step, for example, from the bottom of the column.
- the amount of HF in the in-line feed is greater than that required to form an azeotropic composition with the R-225 da present therein, then the R-225 da content will be —
- a mixture based on HF with a content of less than 225 da, preferably R—HF that is substantially free of 225 da, can be obtained from the recovery section, eg the bottom of the column.
- FIG. 1 is a graph showing the vapor-liquid equilibrium relationship of the HF—R-225 da binary system.
- FIG. 2 is a graph showing the mutual solubility (related to liquid and liquid) of the HF-R-225 da binary system.
- the mixture of HF and R-225 da as feedstocks for such azeotropic distillation may have any composition.
- the content of R-225 da in the mixture is less than 10 mol%, preferably less than 5 mol%.
- the mixture as a feedstock may be separated into two liquid phases, in which case it may be supplied to the distillation step as it is, in a separated state, or after being homogenized by an appropriate means, or Then, only the upper liquid phase or the lower liquid phase may be supplied to the distillation step. Alternatively, each liquid phase may be fed to a separate distillation step.
- the distilling azeotropic composition was separated into an upper liquid phase rich in HF and a lower liquid phase rich in R-225 da by liquid-liquid separation, and these were again subjected to azeotropic distillation. That is, by distilling the lower liquid phase enriched in R-225 da, the azeotropic composition of HF and R-225 da is distilled off, and R-225 substantially free of HF is removed. da can be obtained as a can.
- the upper liquid phase may be similarly distilled, and HF containing substantially no R-225 da can be obtained as a bottom product.
- an azeotropic composition comprising 85-95 mol% HF and 15-5 mol% R-22 ⁇ da is distilled by distilling a mixture comprising HF and R-225 da.
- the azeotropic mixture was separated by distillation to obtain a lower liquid phase rich in R-225 da and an upper liquid phase rich in HF.
- the lower liquid phase was subjected to a distillation step again, and HF and R-225 da were separated.
- the azeotropic composition is removed from the lower liquid phase by distillation, and substantially HF-free R-225 da is protected as bottom product.
- the mixture as a feed material may contain substances other than 11? And 1 ⁇ -22 delta da that do not substantially adversely affect their azeotropes.
- the mixture may contain, for example, HF and a catalyst with a higher boiling point than R-225a, such as a catalyst for producing R-225 da, or the mixture may contain less than R-225 da when producing R-225 da.
- It may be a reaction product containing a reaction raw material.
- the catalyst is, for example, antimony halide. Examples of the reaction raw material include hexaclo-propene and 3,3,3-trifluoro-1,2.2-trichloropropene.
- Such reaction products comprise, for example, 94 mol% of HF and 5 mol% of R-225 da, in addition to these 0.5 mol% of antimony halide, 3,3,3-trifluoro1.2,2-trifluoro Contains 0.5 mol% of mouth propene.
- the liquid is most preferably separated in the range from 20 to 120 ° C. Is carried out. This separation can be easily performed by allowing the mixture to be separated to stand in a normal tank, but a separation-promoting means such as a coalescer for promoting separation is used in the tank. May be provided.
- HF and R-225da form an azeotropic composition at any pressure as long as it is industrially applicable.
- an azeotropic composition of 85 mol% of HF and 15 mol% of R-225 da pressure 3 lKg / cmHabs.
- Azeotropic composition pressure lKgZcni 2 (abs. :), boiling point 18).
- any apparatus can be used as long as it has a function necessary for distillation. It may be a simple distillation apparatus or a rectifying apparatus equipped with a tray or packing. The latter case is particularly preferred. It can be carried out by either batch distillation or continuous distillation.
- Concentrated or purified fluorinated water obtained by distillation The element can be reused, for example, in the production reaction of R-225 da.
- the azeotropic composition consisting of HF and R-225 da can be used as it is as a reflux to return to the distillation step, or can be separated into liquids and used for the next distillation.
- R-225 da obtained from the bottom of the distillation step may be used as it is as a product, or may be subjected to additional treatment, for example, distillation to remove trace impurities.
- Figure 2 plots the measurement results on the horizontal axis, and the vertical axis plots the mol% of HF.
- the liquid in the composition at the center cannot exist as a substantially homogeneous phase, and separates into a homogeneous phase in the rightmost region and a homogeneous phase in the leftmost region.
- the HF concentration of the azeotropic composition consisting of HF and R-225 da is about 10 to 15 mol%, it can be seen from FIG. It can be seen that at 60 ° C, preferably 40-140 ° C, the liquid separates into two phases.
- the lower liquid phase was distilled again.
- the first 3 g of the azeotropic composition was distilled off from the top of the distillation column, and 14 lg of R-225 da (substantially less than 0.05 mol% HF) containing substantially no HF was obtained from the bottom of the column.
- Example 357 g of a distilled azeotropic composition was obtained.
- the azeotropic composition was separated at 20 ° C., and the lower liquid phase rich in R-225 da was taken out to obtain 129 g of a mixture of R-225 da and HF containing 7.5% HF.
- the lower liquid phase was distilled again, and 5 g of an azeotropic composition was removed from the top of the distillation column as an initial distillation to obtain 123 g of R-255 da substantially containing no HF.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE69426837T DE69426837T2 (de) | 1993-12-22 | 1994-12-21 | Verfahren zur reinigung von 1,1,1,3,3-pentafluoro-2,3-dichloropropan |
EP95903913A EP0736508B1 (en) | 1993-12-22 | 1994-12-21 | Process for purifying 1,1,1,3,3-pentafluoro-2,3-dichloropropane |
US08/666,353 US5789632A (en) | 1993-12-22 | 1994-12-21 | Process of purifying 1,1,1,3,3,-pentafluoro-2,3 dichloropropane |
JP51703495A JP3278848B2 (ja) | 1993-12-22 | 1994-12-21 | 1,1,1,3,3−ペンタフルオロ−2,3−ジクロロプロパンの精製方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP5/324710 | 1993-12-22 | ||
JP32471093 | 1993-12-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1995017366A1 true WO1995017366A1 (fr) | 1995-06-29 |
Family
ID=18168849
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1994/002161 WO1995017366A1 (fr) | 1993-12-22 | 1994-12-21 | Procede de purification de 1,1,1,3,3-pentafluoro-2,3-dichloropropane |
Country Status (6)
Country | Link |
---|---|
US (1) | US5789632A (ja) |
EP (1) | EP0736508B1 (ja) |
JP (1) | JP3278848B2 (ja) |
DE (1) | DE69426837T2 (ja) |
ES (1) | ES2156599T3 (ja) |
WO (1) | WO1995017366A1 (ja) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002510664A (ja) * | 1998-04-03 | 2002-04-09 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | 2−クロロ−1,1,1,2,3,3,3−ヘプタフルオロプロパンと、そのhfとの共沸混合物を精製および使用する方法 |
JP2002510665A (ja) * | 1998-04-03 | 2002-04-09 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | 2,2−ジクロロ−1,1,1,3,3,3−ヘキサフルオロプロパンの精製および使用方法 |
JP2012507604A (ja) * | 2008-10-31 | 2012-03-29 | ハネウェル・インターナショナル・インコーポレーテッド | 1,1,1,2,3−ペンタクロロプロパン及びフッ化水素の共沸混合物様組成物 |
JP2015511243A (ja) * | 2012-02-23 | 2015-04-16 | ハネウェル・インターナショナル・インコーポレーテッド | 1,1,3,3−テトラクロロ−1−フルオロプロパンとフッ化水素の共沸組成物 |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6001796A (en) * | 1996-07-03 | 1999-12-14 | Alliedsignal Inc. | Azeotrope-like compositions of 1,1,1,3,3-pentafluoropropane and hydrogen fluoride |
US6900998B2 (en) * | 2002-05-31 | 2005-05-31 | Midwest Research Institute | Variable-speed wind power system with improved energy capture via multilevel conversion |
CN111807925B (zh) * | 2020-07-23 | 2021-11-02 | 山东海益化工科技有限公司 | D-d混剂精馏分离工艺 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02196734A (ja) * | 1989-01-26 | 1990-08-03 | Daikin Ind Ltd | フッ化水素と1,1―ジクロロ―1―フルオロエタンとの混合物から1,1―ジクロロ―1―フルオロエタンを分離する方法 |
JPH03181431A (ja) * | 1989-12-11 | 1991-08-07 | E I Du Pont De Nemours & Co | 2,3―ジクロロ―1,1,1,3,3―ペンタフルオロプロパン及びメタノールの二成分共沸組成物 |
JPH0532568A (ja) * | 1991-07-31 | 1993-02-09 | Daikin Ind Ltd | フツ化水素とジクロロフルオロメタンの混合物からフツ化水素を除去する方法 |
JPH05132434A (ja) * | 1991-04-15 | 1993-05-28 | Daikin Ind Ltd | フツ化水素と1,1,1−トリフルオロ−2−クロロエタンの共沸混合物および1,1,1−トリフルオロ−2−クロロエタンの精製方法 |
-
1994
- 1994-12-21 EP EP95903913A patent/EP0736508B1/en not_active Expired - Lifetime
- 1994-12-21 ES ES95903913T patent/ES2156599T3/es not_active Expired - Lifetime
- 1994-12-21 WO PCT/JP1994/002161 patent/WO1995017366A1/ja active IP Right Grant
- 1994-12-21 JP JP51703495A patent/JP3278848B2/ja not_active Expired - Fee Related
- 1994-12-21 US US08/666,353 patent/US5789632A/en not_active Expired - Fee Related
- 1994-12-21 DE DE69426837T patent/DE69426837T2/de not_active Expired - Fee Related
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02196734A (ja) * | 1989-01-26 | 1990-08-03 | Daikin Ind Ltd | フッ化水素と1,1―ジクロロ―1―フルオロエタンとの混合物から1,1―ジクロロ―1―フルオロエタンを分離する方法 |
JPH03181431A (ja) * | 1989-12-11 | 1991-08-07 | E I Du Pont De Nemours & Co | 2,3―ジクロロ―1,1,1,3,3―ペンタフルオロプロパン及びメタノールの二成分共沸組成物 |
JPH05132434A (ja) * | 1991-04-15 | 1993-05-28 | Daikin Ind Ltd | フツ化水素と1,1,1−トリフルオロ−2−クロロエタンの共沸混合物および1,1,1−トリフルオロ−2−クロロエタンの精製方法 |
JPH0532568A (ja) * | 1991-07-31 | 1993-02-09 | Daikin Ind Ltd | フツ化水素とジクロロフルオロメタンの混合物からフツ化水素を除去する方法 |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002510664A (ja) * | 1998-04-03 | 2002-04-09 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | 2−クロロ−1,1,1,2,3,3,3−ヘプタフルオロプロパンと、そのhfとの共沸混合物を精製および使用する方法 |
JP2002510665A (ja) * | 1998-04-03 | 2002-04-09 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | 2,2−ジクロロ−1,1,1,3,3,3−ヘキサフルオロプロパンの精製および使用方法 |
JP2012507604A (ja) * | 2008-10-31 | 2012-03-29 | ハネウェル・インターナショナル・インコーポレーテッド | 1,1,1,2,3−ペンタクロロプロパン及びフッ化水素の共沸混合物様組成物 |
JP2015511243A (ja) * | 2012-02-23 | 2015-04-16 | ハネウェル・インターナショナル・インコーポレーテッド | 1,1,3,3−テトラクロロ−1−フルオロプロパンとフッ化水素の共沸組成物 |
Also Published As
Publication number | Publication date |
---|---|
EP0736508A1 (en) | 1996-10-09 |
US5789632A (en) | 1998-08-04 |
DE69426837D1 (de) | 2001-04-12 |
EP0736508A4 (en) | 1997-04-02 |
ES2156599T3 (es) | 2001-07-01 |
EP0736508B1 (en) | 2001-03-07 |
JP3278848B2 (ja) | 2002-04-30 |
DE69426837T2 (de) | 2001-07-19 |
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