WO2004000734A1 - 含フッ素乳化剤の回収方法 - Google Patents
含フッ素乳化剤の回収方法 Download PDFInfo
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- WO2004000734A1 WO2004000734A1 PCT/JP2003/007772 JP0307772W WO2004000734A1 WO 2004000734 A1 WO2004000734 A1 WO 2004000734A1 JP 0307772 W JP0307772 W JP 0307772W WO 2004000734 A1 WO2004000734 A1 WO 2004000734A1
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- aqueous liquid
- acid
- fluorinated emulsifier
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F14/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F14/18—Monomers containing fluorine
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
- C02F2101/14—Fluorine or fluorine-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
- C02F2101/325—Emulsions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/06—Pressure conditions
- C02F2301/063—Underpressure, vacuum
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Definitions
- the present invention relates to a method for recovering a fluorinated emulsifier using a vacuum concentration method.
- IER anion exchange resin
- JP-B-47-51233 describes a method of coagulating and washing latex of emulsion polymerization, collecting an emulsifier as an aqueous solution, evaporating the obtained aqueous solution to dryness, and recovering the fluorinated emulsifier with an organic solvent.
- the text also describes a method of recovering the fluorinated emulsifier using an ion exchange resin.
- US Pat. No. 4,282,162 describes a method in which a dilute emulsifier aqueous solution is brought into contact with a weakly basic anion exchange resin in the pH range of 0 to 7, the emulsifier is adsorbed, and desorbed with ammonia water.
- a nonionic or thiothionic surfactant is added to the coagulated waste water of the fluoropolymer to stabilize the polytetrafluoroethylene (hereinafter referred to as PTFE) fine particles in the coagulated waste water, A method for preventing clogging of packed columns is described.
- PTFE polytetrafluoroethylene
- JP-A-55-120630, US Pat. No. 4,369,266 and DE2908001 describe a part of ammonium perfluorooctanoate (hereinafter referred to as APFO) used for concentrating PTFE coagulated wastewater by ultrafiltration and producing PTFE.
- APFO ammonium perfluorooctanoate
- JP-A-55-104651 US Pat. No. 4,282,162 and DE2903981 disclose a method of adsorbing APFO to IER and then desorbing and recovering perfluorooctanoic acid using a mixture of an acid and an organic solvent.
- WO 99/62858 states that after adding lime water to the coagulated waste water of tetrafluoroethylene Z perfluoro mouth (alkyl vinyl ether) copolymer (hereinafter referred to as PFA), the pH is adjusted to 6 to 7.5.
- metal salts such as aluminum chloride and iron chloride are added to agglomerate the unagglomerated PFA, and then the aggregates are mechanically separated and removed.
- the pH of the obtained wastewater is adjusted to 7 or less with sulfuric acid.
- Japanese Patent Application Laid-Open No. 2001-62313 describes a method for desorbing APFO adsorbed on IER using a mixed solution of water, alkali and organic solvent.
- Japanese Patent Application Laid-Open No. 2002-59160 discloses a method for desorbing a fluorine-containing emulsifier adsorbed on an IER using a mixed solution of water, alcohol (especially sodium hydroxide), and an organic solvent (especially methanol, ethanol, and acetate). Has been described.
- JP-A-2002-58966 describes a method for concentrating and recovering a fluorine-containing emulsifier using a reverse osmosis membrane.
- WO 02/10104 A1 and WO 02/10105 A1 are prepared by adding a divalent metal and a trivalent metal to an aqueous solution containing a fluorinated emulsifier to form a layered double hydroxide. A method for recovery is described.
- the present invention has been made in view of the above circumstances, and it is an object of the present invention to provide a method for efficiently recovering a fluorinated emulsifier from a low-concentration aqueous liquid such as coagulated waste water of a fluorinated polymer by a simple method. Disclosure of the invention
- the present invention provides an aqueous liquid (A) in which the concentration of the fluorinated emulsifier is 1 mass% or more and 1 mass% or less, a pressure of 100 kPa or less, and a temperature of the aqueous liquid (A) of 100 ° C.
- the concentration of the fluorinated emulsifier in the aqueous liquid (B) is 5% by mass or more in order to efficiently recover the fluorinated emulsifier at a high recovery rate.
- the concentration of the fluorinated emulsifier in the aqueous liquid (A) is from 1% by mass to 1% by mass, preferably from 10% by mass to 1% by mass, particularly preferably from 10% by mass to 500% by mass. 0 mass ppm or less is preferable.
- the concentration of the fluorinated emulsifier in the aqueous liquid (A) is too low, a large amount of water is required to concentrate the highly concentrated aqueous liquid (B), particularly the aqueous liquid (B) having the preferred concentration of the fluorinated emulsifier (5% by mass or more). Energy is needed. If the concentration of the fluorine-containing emulsifier in the aqueous liquid (A) is too high, the meaning of the specific vacuum concentration in the present invention is lost. In the case of such a high concentration, for example, The fluorinated emulsifier can be recovered by a simpler and more efficient method such as precipitation of the fluorinated emulsifier by changing pH.
- the aqueous liquid (A) used in the step of producing a fluorine-containing polymer obtained by emulsion polymerization or aqueous dispersion polymerization of at least one fluorine-containing monomer in an aqueous medium containing a fluorine-containing emulsifier is used.
- An aqueous solution containing the fluorinated emulsifier obtained by washing the waste water after separating the fluoropolymer (A 1) and the waste gas from the drying step and / or the heat treatment step of the fluoropolymer with the aqueous liquid (A 2) ) Is preferably at least one aqueous liquid selected from the group consisting of:
- the wastewater (A 1) after the separation of the fluoropolymer is usually preferably coagulated wastewater of the fluoropolymer after emulsion polymerization or aqueous dispersion polymerization, and is particularly preferably a polymer of a fluoromonomer or a fluoromonomer. Coagulated wastewater from the process of producing a copolymer with a monomer other than the fluorine-containing monomer is preferred.
- the coagulated waste water from the production process is a fluorine-containing monomer, or a monomer other than a fluorine-containing monomer and a fluorine-containing monomer, which is subjected to emulsion polymerization or aqueous dispersion polymerization in an aqueous medium containing a fluorine-containing emulsifier.
- This refers to waste water after the fluoropolymer is aggregated from the obtained aqueous dispersion of the fluoropolymer by salting out or the like and the fluoropolymer is separated.
- the wastewater contains the fluorine-containing emulsifier used during the polymerization of the fluorine-containing monomer, and also contains an SS content such as a non-aggregated fluorine-containing polymer.
- coagulated wastewater hereinafter, sometimes referred to as coagulated wastewater (aA)
- A aqueous liquid
- the exhaust gas in the aqueous f night (A 2) the exhaust gas in the drying step and the Z or heat treatment step of the fluoropolymer, which is usually obtained by emulsion polymerization or aqueous dispersion polymerization in an aqueous medium containing a fluorine-containing emulsifier, Is preferred.
- an aqueous solution of a fluorine-containing polymer obtained by emulsion polymerization or aqueous dispersion polymerization of a fluorine-containing monomer or a fluorine-containing monomer and a monomer other than a fluorine-containing monomer in an aqueous medium containing a fluorine-containing emulsifier is used.
- the fluoropolymer is coagulated and separated from the dispersion by salting out or the like, and when the separated fluoropolymer is dried and Z or heat-treated using a heat treatment device such as an oven, the fluorine-containing polymer is separated from the heat treatment device.
- Discharged Exhaust gas containing a small amount of solid droplets.
- the aqueous liquid (A 2) may be referred to as an aqueous liquid containing a fluorinated emulsifier obtained by washing the exhaust gas with the aqueous liquid (hereinafter, may be referred to as an aqueous liquid (A 2 a)). This will be described as a representative.
- a suspended solid such as an unagglomerated fluoropolymer contained in the coagulated wastewater (a A), or a metal salt used for salting-out and coagulation of the fluoropolymer, and a change in pH of the coagulated wastewater.
- Substances that can become suspended solids such as substances that precipitate and substances that precipitate when the temperature of the coagulated wastewater falls or rises (hereinafter, suspended solids and substances that can become suspended solids are collectively referred to as SS content).
- the content of SS is preferably set to 0.3% by mass or less, and particularly preferably 0.05% by mass, since it may adhere to the inside of the concentration device during the vacuum concentration in the present invention and reduce the thermal efficiency. % Is more preferable.
- An effective method of removing the SS content of unagglomerated fluoropolymers is to add a metal salt (a salting-out agent) containing a polyvalent metal cation to aggregate the SS content.
- metal salts include aluminum chloride, aluminum chloride hexahydrate, magnesium chloride, magnesium chloride hexahydrate, ferrous chloride, ferric chloride, ferric chloride hexahydrate, and polychlorinated chloride.
- Metal chlorides such as aluminum are exemplified.
- the pH is adjusted to 7 or more by adding sodium hydroxide and Z or a hydroxylating lime. It is preferable that the fluorinated emulsifier is redissolved from the aggregate in water.
- the coagulated waste water (aA) is preferably stirred.
- the stirring method is not particularly limited, but a method using a stirrer that does not mechanically destroy the aggregate particles generated by stirring is preferable.
- the stirring blade of the stirring device is preferably a stirring blade capable of uniformly mixing the entire coagulated waste water (aA) at a low rotation speed, and is preferably one member selected from the group consisting of a full zone blade, a max blend blade and an amplifier blade.
- G value during stirring at the stirring blade is preferably from 1 to 3 0 0 s-1, more preferably 5 ⁇ 2 5 0 s- 1, 1 0 ⁇ 2 0 0 s _ 1 is most preferred.
- the G value is a value derived from the following equation. One.
- ⁇ stirring power (W)
- V liquid volume (m 3 )
- Pa * s liquid viscosity coefficient
- a general solid-liquid separation method can be adopted as a method for removing the aggregated SS component.
- the filtration is also preferably performed under pressure.
- it is preferable that the wastewater containing the aggregates is allowed to stand still, the aggregates are settled, and the supernatants are filtered to remove the aggregates.
- a solid-liquid separation method using a thickener or a screw decanter is most preferable.
- the aqueous liquid (A) is concentrated under reduced pressure at a pressure of 10 OkPa or lower.
- the pressure is preferably 50 kPa or less, particularly preferably 30 kPa or less. If the pressure is too large, a high temperature is required to evaporate the solvent containing water as a main component, so that not only the required energy cannot be reduced sufficiently, but also the fluorine-containing emulsifier is used in the solvent due to the high temperature. Loss may be caused by flying together.
- the temperature of the aqueous liquid (A) is adopted to be 100 ° C. or less.
- the temperature is preferably at most 80 ° C. If the temperature is too high, not only the required energy cannot be reduced sufficiently, but also because of the high temperature, the fluorinated emulsifier may be lost due to scattering along with the solvent.
- the temperature fluctuation be within the set temperature ⁇ 2.
- an antifoaming agent such as silicone.
- an antifoaming agent is preferably avoided as much as possible because it may adversely affect the physical properties of the regenerated fluorinated emulsifier.
- the device used for vacuum concentration is a device that uses steam generated by evaporation. Devices that can be efficiently reused to reduce energy consumption are preferred.
- the apparatus for performing the decompression concentration may be configured such that the amount of energy required for evaporating the unit liquid of the aqueous liquid (A) per unit volume under atmospheric pressure is equal to the amount of energy required for evaporating the same unit volume at atmospheric pressure. It is preferable to use a reduced-pressure concentrator having a concentration of 50% or less. Examples of such a device include a heating tube surface evaporation type concentrator equipped with a heat pump and a flash type concentrator equipped with Z or an ejector.
- the coagulated wastewater A is heated at a pressure of 100 kPa or lower. And is sprayed from the upper part of the heating evaporator to the heating tube portion by the circulation pump together with the circulating liquid in the heating evaporator, and the thin film evaporates on the surface of the heating tube portion. At this time, foaming can be suppressed by spraying a part of the circulating liquid near the surface of the liquid held in the heating evaporator.
- the vapor evaporated on the surface of the heating tube is compressed by a heat pump, and the temperature is raised by 3-6.
- the steam whose temperature has risen is introduced into the inside of the heating pipe, evaporates the circulating fluid sprayed outside the heating pipe, becomes condensed water, and is discharged out of the system by the condensed water pump.
- a heating tube surface evaporating type concentrating device equipped with a heat pump a VVCC concentrating device or an EVCC concentrating device manufactured by Sasakura can be exemplified.
- the concentration of the fluorinated emulsifier can be increased to 5% by mass or more, or even 10% by mass or more, using a heating tube surface evaporation type concentrator equipped with the above-mentioned heat pump.
- a heating tube surface evaporation type concentrator equipped with the heat pump since the heating tube surface evaporation type concentrator equipped with the heat pump has a large number of heating tubes inside, when the concentration of the fluorinated emulsifier increases, the structure of the heating tube becomes fluorinated. Thermal efficiency may be reduced due to precipitation of emulsifier or adhesion of SS in coagulated wastewater (a A).
- the concentration of the fluorinated emulsifier is usually limited to about 100 mass ppm to 5 mass%, particularly about 0.5 mass% to 3 mass%, in the concentration by the heating tube surface evaporating concentration apparatus equipped with the heat pump. preferable.
- the concentration of the aqueous liquid (A) under reduced pressure may be performed using a flash-type concentrator (hereinafter, may be simply referred to as a flash evaporator).
- a flash-type concentrator equipped with an ejector for example, an FTC concentrator manufactured by Sasakura, etc. can be used) can also be used.
- these flash type concentrators do not have a problem due to a high concentration of the fluorinated emulsifier as in the above-mentioned heating evaporator, they are usually used for concentrating an aqueous liquid containing a fluorinated emulsifier having reached a relatively high concentration. It is preferably used.
- the vacuum concentration of the aqueous liquid (A) in the present invention is preferably performed in two or more stages.
- the first stage is performed using a heating tube surface evaporating concentrator equipped with a heat pump
- the second and subsequent stages are performed using a heating tube surface evaporating concentrator or a flash type concentrator equipped with a heat pump.
- the first step is performed using a heating tube surface evaporation type concentrator equipped with a heat pump
- the second and subsequent steps are performed using a flash type concentrator.
- the aqueous liquid of the fluorinated emulsifier which has been concentrated in the heating evaporator to reach a relatively high concentration is further concentrated using a flash evaporator.
- a flash evaporator For example, when an aqueous liquid of a fluorinated emulsifier that has reached a relatively high concentration is introduced into a flash evaporator kept at 30 kPa or less, the inside of the flash evaporator is introduced due to reduced pressure. The aqueous liquid flash evaporates.
- a part of the evaporated vapor is sucked into the ejector using a flash-type concentrator equipped with an ejector such as the FTC concentrator, and the circulating liquid is removed by the heater together with the driving steam for the ejector. It can be used as a heating source.
- the condensed water discharged by the vacuum concentration operation in the present invention is used for washing the exhaust gas from the fluoropolymer drying step and Z or the exhaust gas from the heat treatment step to obtain the aqueous solution (A 2 a).
- the concentration of the fluorinated emulsifier in the aqueous liquid (B) obtained in the vacuum concentration step is higher than that in the aqueous liquid (A).
- the concentration of the fluorinated emulsifier in the aqueous liquid (B) is preferably at least 5% by mass, more preferably at least 10% by mass.
- Concentration of fluorinated emulsifier in aqueous liquid (B) When the content is within the above range, the recovery of the fluorinated emulsifier in the present invention can be 90% by mass or more. If the concentration of the fluorinated emulsifier in the aqueous liquid (B) is too low, only the solubility of the free acid of the fluorinated emulsifier in water cannot be recovered. Recovery rate cannot be increased sufficiently.
- the upper limit of the concentration of the fluorine-containing emulsifier is not necessarily limited, but is preferably 50% by mass or less.
- the fluorinated emulsifier having a high concentration in the aqueous liquid (B) can be precipitated in the form of a free acid by making the aqueous liquid (B) acidic at pH 4 or less.
- the precipitated free acid can be collected by filtration.
- the aqueous liquid (B) may be made acidic for the purpose of purifying the fluorine-containing emulsifier, and it may be easily extracted with a water-insoluble organic solvent in a state where a precipitate is formed.
- water-insoluble organic solvent examples include chloroform, dichloroethylene, methylene chloride, hexane, benzene, toluene, R-113, R-225 ca, R-225 cb, R-123 , R- 141 b, can be mentioned at least one kind of solvent selected Ri by the group consisting of C 6 F 1 3 H and C 8 F, 8. Particularly, in view of the solubility of the free acid in the solvent, R-113, R-225 ca, R-225 cb, R-123, R-141 b, C 6 F x 3 even without less selected from the group consisting of H and C 8 F x 8 is one non water-soluble fluorine-containing organic solvents preferred.
- the free acid extracted in the solvent can be purified by removing impurities containing no fluorine by distillation with the solvent.
- chloroform-form, dichloroethylene, methylene chloride, hexane, benzene, toluene, R-113, R-225 ca, R-225 cb, R-123, R-141 b recrystallization of the free acid using at least one solvent selected from the group consisting of C 6 F 13 H and C 8 F, 8 to remove and purify fluorine-containing impurities. be able to.
- the recovery of the fluorine-containing emulsifier from the aqueous liquid (B) is particularly preferably performed by an extraction method using the non-water-soluble fluorine-containing organic solvent.
- the purified fluorinated emulsifier is reused as an emulsifier for fluorinated polymer polymerization. Can be used.
- the fluorinated emulsifier may be a salt having 5 to 13 carbon atoms, such as perfluoroalkanoic acid, ⁇ -hydroperfluoroalkanoic acid, ⁇ -chloroperfluoroalkanoic acid, or perfluoroalkanesulfonic acid. These are preferably a linear or branched structure, or a mixture thereof. Further, the molecule may contain an etheric oxygen atom. When the number of carbon atoms is in this range, the effect as an emulsifier is excellent.
- the acid salt is preferably an alkaline metal salt such as a lithium salt, a sodium salt, or a potassium salt, or an ammonium salt, more preferably an ammonium salt or a sodium salt, and most preferably an ammonium salt.
- the acid include perfluoropentanoic acid and perfluorohexanoic acid.
- Perfluoroheptanoic acid perfluorooctanoic acid, perfluorononanoic acid, perfluorodecanoic acid, perfluorododecanoic acid, ⁇ -hydroperfluoroheptanoic acid, ⁇ _hydro Perfluorooctanoic acid, ⁇ _hydroperfluorononanoic acid, ⁇ -chloroperfluoroheptanoic acid, ⁇ -chloroperfluorooctanoic acid, ⁇ monochloroperfluorononanoic acid, etc. Is mentioned.
- the acid include CF 3 CF 2 CF 2 OCF (CF 3 ) COO H, CF 3 CF 2 CF 2 OCF (CF 3 ) CF 2 OCF (CF 3 ) CO ⁇ H, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 2 CF (CF 3 ) COOH, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 3 CF (CF 3 ) COOH, CF 3 CF 2 CF 2 CF 2 CF 2 OCF (CF 3 ) C ⁇ OH and the like can also be mentioned.
- perfluorohexanesulfonic acid perfluoroheptansulfonic acid, perfluorooctanesulfonic acid, perfluorononanesulfonic acid, perfluorononsulfonic acid, and the like are also included.
- ammonium salt examples include ammonium perfluoropentanoate, ammonium perfluorohexanoate, ammonium perfluoroheptanoate, ammonium perfluorooctanoate (APFO), and perfluorononanoate.
- ammonium salt examples include CF 3 CF 2 CF 2 OCF (CF 3 ) COONH 4 , CF 3 CF 2 CF 2 OCF (CF 3 ) CF 2 OCF (CF 3) COONH 4 , CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 ⁇ ] 2 CF (CF 3 ) COONH 4 , CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 3 CF (CF 3 ) COONH 4 , CF 3 CF 2 CF 2 CF 2 OCF (CF 3 ) COONH 4 , CF 3 CF 2 CF 2 CF 2 OCF (CF 3 ) COONH 4 and the like.
- ammonium perfluorohexane sulfonate ammonium perfluoroheptanesulfonic acid, ammonium perfluorooctane sulfonate, ammonium perfluorononane sulfonate, ammonium perfluorodecane sulfonate, etc.
- ammonium perfluorohexane sulfonate ammonium perfluoroheptanesulfonic acid
- ammonium perfluorooctane sulfonate ammonium perfluorononane sulfonate
- ammonium perfluorodecane sulfonate etc.
- lithium salt examples include lithium perfluoropentanoate, lithium perfluorohexanoate, lithium perfluoroheptanoate, lithium perfluorosiloxane, lithium perfluorononanoate, and lithium perfluoronate.
- lithium salt examples include CF 3 CF 2 CF 2 OCF (CF 3 ) COOL i, CF 3 CF 2 CF 2 OCF (CF 3 ) CF 2 OCF (CF 3 ) COOL i, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 2 CF (CF 3 ) COOL i, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 ⁇ ] 3 CF (CF 3 ) COOL i, CF 3 CF 2 CF 2 CF 2 OCF (CF 3 ) COOL i.
- lithium perfluorohexane sulfonate lithium perfluoroheptane sulfonate, lithium perfluorooctane sulfonate,
- lithium fluorononane sulfonate lithium perfluorodecane sulfonate and the like can be mentioned.
- sodium salt examples include sodium perfluoropentanoate, sodium perfluorohexanoate, sodium perfluoroheptanoate, sodium perfluorooctanoate, sodium perfluorononanoate, sodium perfluorodecanoate Sodium perfluorododecanoate, sodium ⁇ -hydroperfluoroheptanoate, sodium ⁇ -hydroperfluorooctanoate, ⁇ -sodium hydroperfluorononanoate, ⁇ -sodium sodium perfluoroheptanoate, ⁇ -clo mouth sodium perfluorooctanoate, ⁇ -clo mouth sodium perfluorononanoate and the like.
- sodium salt examples include CF 3 CF 2 CF 2 OCF (CF 3) COONa, CF 3 CF 2 CF 2 OCF (CF 3 ) CF 2 OCF (CF 3 ) COONa, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 2 CF (CF 3 ) COONa, CF 3 CF 2 CF 2 ⁇ [CF (CF 3 ) CF 2 O] 3 CF (CF 3) COONa, CF 3 CF 2 CF 2 CF 2 CF 2 OCF (CF 3 ) COON a and the like.
- sodium perfluorohexanesulfonic acid sodium perfluoroheptanesulfonic acid, sodium perfluorooctanesulfonic acid, sodium perfluorononanesulfonic acid, sodium perfluorononanesulfonic acid, and the like are also available. No.
- potassium salt examples include potassium perfluoropentanoate, potassium perfluorohexanoate, potassium perfluoroheptanoate, potassium perfluorooctanoate, potassium perfluorononanoate, perfluoropentanoate Potassium rodecanoate, potassium perfluorododecanoate, potassium ⁇ -hydroperfluoroheptanoate, potassium ⁇ -hydroperfluorooctanoate, ⁇ -potassium hydroperfluorononanoate, ⁇ And potassium ⁇ -chloroperfluoroheptanate, potassium ⁇ -chloroperfluorononanoate, and ⁇ -chloroperfluorononanoic acid potassium.
- a specific example of the potassium salt is CF 3 CF.
- CF 2 OCF (CF 3 ) COOK CF 3 CF 2 CF 2 OCF (CF 3 ) CF 2 OCF (CF 3 ) CO OK, CF 3 CF 2 CF 2 O [CF (CF 3 ) CF 2 O] 2 CF (CF 3 ) CO OK, CF 3 CF 2 CF 2 ⁇ [CF (CF 3) CF 2 O] 3 CF (CF 3) CO OK, CF 3 CF 2 CF 2 CF 2 CF 2 OCF (CF 3) COOK , etc. Ru also mentioned.
- Perfluorohexane sulfonate potassium perfluoroheptanesulfonate, potassium perfluorooctanesulfonate, perfluorononane sulfonate, perfluorodesulfonic acid, and the like.
- an ammonium salt of a perfluoroalkanoic acid having 6 to 12 carbon atoms is particularly preferable, and ammonium perfluorohepnoate, APFO, ammonium perfluorononanoate or perfluorodeacid. Ammonia is more preferred, and APF is most preferred.
- TFE tetrafluoroethylene
- CF 2 CFC 1
- CFH CF 2
- CH 2 CH 2
- VdF CF 2
- Furuoroechiren such, the hexa full O b propylene (hereinafter,.
- HEP CF full O b propylene
- 2 CHCF 3
- CF 2 CFOCF 3
- CF 2 CFO (CF 2) 2 CF 3
- PPVE Perfluoro vinyl ethers having 3 to 10 carbon atoms
- CF 2 CFO (CF 2 ) 4 CF 3
- fluorinated monomers may be used alone or in combination of two or more.
- Monomers other than the fluorine-containing monomer include vinyl esters such as vinyl acetate, vinyl ethers such as ethyl vinyl ether, cyclohexyl vinyl ether and hydroxybutyl vinyl ether, and monomers having a cyclic structure such as norbornene and norponagen. Examples thereof include aryl ethers such as methyl aryl ether, and olefins such as ethylene (hereinafter, referred to as E), propylene (hereinafter, referred to as P), and isobutylene. Monomers other than the fluorinated monomer may be used alone or in combination of two or more.
- the fluoropolymer is not particularly limited, but is preferably At least one selected from the group consisting of PTFE, TFE / P copolymer, TFEZP / VdF copolymer, TFE / HFP copolymer, TFE / PPVE copolymer, EZTFE copolymer and polyvinylidene fluoride is there. More preferably, it is PTFE, TFE / P copolymer, TFEZP VdF copolymer or TFE / PPVE copolymer, most preferably PTFE.
- the method for recovering a fluorinated emulsifier of the present invention is particularly useful for the aqueous liquid (A) in which the concentration of the fluorinated emulsifier is 1 mass ppm or more and 1 mass% or less. (More than 1% by mass to less than 5% by mass). That is, the aqueous solution containing a relatively low concentration of the fluorinated emulsifier can be made to have a high concentration (for example, 5% by mass or more, particularly 10% by mass or more) by vacuum concentration in the present invention.
- the method for recovering a fluorinated emulsifier of the present invention may include, in addition to the fluorinated emulsifier, a low-molecular-weight fluorinated carboxylic acid such as trifluoroacetic acid and pentafluoropropanoic acid and / or a salt thereof, trifluoromethanesulfonic acid and / or a salt thereof. Also applicable to salt and the like.
- a low-molecular-weight fluorinated carboxylic acid such as trifluoroacetic acid and pentafluoropropanoic acid and / or a salt thereof, trifluoromethanesulfonic acid and / or a salt thereof. Also applicable to salt and the like.
- the concentration of APFO, perfluorooctanoic acid or sodium perfluorooctanoate was measured by a high-performance liquid chromatography-mass spectral method using a mixed solution of methanol and water as a solvent. Species to be detected by this method is base Le full O Roo Kuta Noe Ichito (C 7 F 1 5 COO " ).
- Coagulated wastewater after emulsion polymerization of PTFE (SS content: 230 ppm. Mark water 1.
- the AP FO concentration was measured and found to be 208 ppm.
- the APFO-containing wastewater from which PTFE has been removed in advance (hereinafter simply referred to as the wastewater) is concentrated under reduced pressure using a heating-tube-surface evaporation-type concentrator equipped with a heat pump (trade name: E VCC concentrator, manufactured by Sasakura). I let it.
- the supply amount of the wastewater was 50 LZ, and the inside of the EVCC concentrator was kept at 20 kPa.
- the temperature of the circulating fluid inside the EVCC concentrator was maintained at 65 ⁇ 2 ° C. Immediately after the start of operation, the liquid inside the EVCC concentrator started foaming, but did not generate a large amount of liquid.
- 750 L of the wastewater was introduced into an EVCC concentrator to obtain 20 L of 37.5-fold concentrated water.
- the evaporating water was condensed, collected in full, and analyzed to find that the APFO concentration was lppm. From this, APFO lost by vacuum concentration using the EVCC concentrator was 0.48% (0.73 g).
- the energy used in the EVCC concentrator was 3.42 kW.
- the 37.5-fold concentrated water concentrated by the EVCC concentrator was further concentrated using a flash-type concentrator equipped with an ejector (manufactured by Sasakura, trade name: FTC concentrator).
- FTC concentrator manufactured by Sasakura, trade name: FTC concentrator.
- the pressure inside the FTC concentrator was kept at 20 kPa.
- the temperature was kept at 50 ⁇ 2 ° C.
- 20 L of the 37.5-fold concentrated water was concentrated to 1.0 L of 750-fold concentrated water. All of the condensed water discharged from this FTC concentrator was collected and the APFO concentration was measured. From this, the APFO lost by the FTC concentrator was 0.013% (0.019 g).
- the energy used in the FTC concentrator was 28.2 kW.
- the APFO concentration in the 750-fold concentrated water was 15.0%.
- the 750-fold concentrated water was cloudy, and a white precipitate was found at about 16% by volume. pH was 11.9.
- the pH was adjusted to 1 by adding concentrated sulfuric acid to the 750-fold concentrated water. During the addition of sulfuric acid, the mixture was stirred with an anchor blade. From the point in time when the pH fell below 4, a large amount of white suspended matter began to be generated in the concentrated water. After adjusting the pH to 1, the mixture was stirred for 30 minutes. 100 g of R-225 cb was added to the concentrated water adjusted to this pH1. The white precipitate generated in the concentrated water was dissolved in the R-225 cb phase.
- the R-225cb phase was separated and the entire amount of R-225cb was evaporated at room temperature to give 143.lg as a white solid.
- this white solid was perfluorooctanoic acid.
- the recovery rate of APFO in the enrichment operation using this EVCC enrichment unit and FTC enrichment unit is 99%.
- PTFE produced by emulsion polymerization using APFO as an emulsifier was agglomerated.
- This water-containing PTFE powder (10.0 kg, water content: 48% by mass) was placed in a hot-air circulation oven, heated at a rate of 100 to 51: / min over time, and then heat-treated at 200 ° C for 1 hour.
- the amount of exhaust gas discharged from the hot-air circulation oven was 4.5 Nm 3 Zh.
- the entire amount of the exhaust gas was introduced into a spray tower having a diameter of 50 cm and a height of 500 cm.
- the linear velocity of the gas at this time was about 0.5 m / sec.
- the spray tower 35 kg of ion-exchanged water whose pH was adjusted to 10 using sodium hydroxide was circulated and sprayed. After the drying and heat treatment of the PTFE powder, the APF O concentration in the alkaline water in the spray tower was analyzed, and was 498 mass ppm.
- a 0.2 N aqueous sodium hydroxide solution was added to adjust the pH to 10.0.
- the liquid temperature was 26 ° C.
- the APFO-containing wastewater was concentrated under reduced pressure by a heating tube surface evaporation type concentrator equipped with a heat pump (trade name: EVCC concentrator manufactured by Sasakura).
- the supply rate of the wastewater containing APFO was 10 L / hour, and the inside of the EVCC concentrator was maintained at 20 kPa.
- the temperature of the circulating fluid inside the EVCC concentrator was kept at 65 ⁇ 2.
- the 17.5-fold concentrated water concentrated by this EVCC concentrator was further concentrated using a single-tally evaporator. Reduce the pressure inside the rotary evaporator to 2
- the temperature was kept at 50 ⁇ 2 ° C.
- the 17.5-fold concentrated water was concentrated to 0.15 L of the 233-fold concentrated water over 2 hours.
- the APFO lost by the rotary evaporator was 0.013% (0.0024 g).
- the energy used on the rotary evaporator was 1.40 kW.
- the APFO concentration in the 233-fold concentrated water was 11.6%.
- the 233-fold concentrated water was cloudy, and a white precipitate was found at about 17% by volume. pH was 11.4.
- Concentrated sulfuric acid was added to the 233-fold concentrated water to adjust the pH to 1. During the addition of sulfuric acid, the mixture was stirred with an anchor blade. From the point in time when the pH fell below 4, a large amount of white suspended matter began to be generated in the concentrated water. After adjusting the pH to 1, the mixture was stirred for 30 minutes. 10 g of n—C 8 F, 8 was added to the concentrated water adjusted to pH. White precipitation occurred concentrated water were dissolved in n- C 8 F, 8 phase. The nC 8 F x 8 phase was separated, the total amount of nC 8 8 evaporated at room temperature to obtain a white solid 16. 5 g. As a result of infrared spectroscopy, this white solid was perfluorooctanoic acid. The recovery rate of APFO in this enrichment operation using EVCC and a rotary evaporator was 99%
- the APFO-containing wastewater was concentrated using a flash-type concentrator equipped with an ejector (trade name: FTC concentrator manufactured by Sasakura). During the concentration operation, the pressure inside the FTC concentrator was kept at 20 kPa. The temperature was kept at 60 ⁇ 2. 1 Over 200 hours, 200 L of the wastewater containing APFO was concentrated to 1.0 L of 200 times concentrated water. The total amount of condensed water discharged from this FTC concentrator was collected, and the APFO concentration was measured. From this, APFO lost by the FTC concentrator was 0.13% (0.198 g). The energy used in the FTC concentrator was 154.4 kW. The APFO concentration of this 200-fold concentrate was 15.6%.
- the 200-fold concentrated water was cloudy, and a white precipitate was observed at about 16% by volume. pH was 11.2.
- Concentrated sulfuric acid was added to the 200-fold concentrated water to adjust 11 to 1. During the addition of sulfuric acid, the mixture was stirred with an anchor blade. From the point in time when the pH fell below 4, a large amount of white suspended matter began to be generated in the concentrated water. After the pH was adjusted to 1, the mixture was stirred for 30 minutes. 100 g of R-225 cb was added to the concentrated water adjusted to pH. The white precipitate generated in the concentrated water was dissolved in the R-225 c b phase.
- the R-225cb phase was separated, and the entire amount of R-225cb was evaporated at room temperature to obtain 148.6 g of a white solid.
- this white solid was perfluorooctanoic acid.
- the recovery of APFO in the concentration operation using this FTC concentrator was 99%.
- the concentration of A PFO in the coagulated waste water (containing 2300 ppm of SS) after emulsion polymerization of PTF E was 148 ppm.
- 65.0 g of aluminum chloride hexahydrate was added to 1000 of the coagulated waste water to coagulate uncoagulated PTFE particles.
- the pH of the waste water was adjusted to 10.0 using 0.2N sodium hydroxide.
- the supernatant of the drainage was colorless and transparent, and the SS content was 2 O ppm.
- the concentration of APFO in the supernatant of the wastewater was 141 ppm.
- a fluorinated emulsifier can be efficiently and easily recovered from flocculated waste water of a fluorinated polymer. Also, compared to known recovery methods, there is no need to add another chemical substance and the recovery efficiency is high.
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
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Abstract
Description
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Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
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DE60304469T DE60304469T2 (de) | 2002-06-19 | 2003-06-19 | Verfahren zur gewinnung von fluor-enthaltenden emulgatoren |
JP2004515513A JP4455327B2 (ja) | 2002-06-19 | 2003-06-19 | 含フッ素乳化剤の回収方法 |
EP03760892A EP1514848B1 (en) | 2002-06-19 | 2003-06-19 | Process for the recovery of fluorine-containing emulsifiers |
AU2003244295A AU2003244295A1 (en) | 2002-06-19 | 2003-06-19 | Process for the recovery of fluorine-containing emulsifiers |
US11/012,334 US7351342B2 (en) | 2002-06-19 | 2004-12-16 | Method for recovering fluorine-containing emulsifier |
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JP2002-178728 | 2002-06-19 | ||
JP2002178728 | 2002-06-19 |
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US11/012,334 Continuation US7351342B2 (en) | 2002-06-19 | 2004-12-16 | Method for recovering fluorine-containing emulsifier |
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WO2004000734A1 true WO2004000734A1 (ja) | 2003-12-31 |
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US (1) | US7351342B2 (ja) |
EP (1) | EP1514848B1 (ja) |
JP (1) | JP4455327B2 (ja) |
CN (1) | CN100381366C (ja) |
AU (1) | AU2003244295A1 (ja) |
DE (1) | DE60304469T2 (ja) |
RU (1) | RU2315718C2 (ja) |
WO (1) | WO2004000734A1 (ja) |
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- 2003-06-19 EP EP03760892A patent/EP1514848B1/en not_active Expired - Fee Related
- 2003-06-19 WO PCT/JP2003/007772 patent/WO2004000734A1/ja active IP Right Grant
- 2003-06-19 CN CNB038142651A patent/CN100381366C/zh not_active Expired - Lifetime
- 2003-06-19 AU AU2003244295A patent/AU2003244295A1/en not_active Abandoned
- 2003-06-19 RU RU2005101086/15A patent/RU2315718C2/ru not_active IP Right Cessation
- 2003-06-19 DE DE60304469T patent/DE60304469T2/de not_active Expired - Lifetime
- 2003-06-19 JP JP2004515513A patent/JP4455327B2/ja not_active Expired - Fee Related
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JP2007099624A (ja) * | 2005-09-30 | 2007-04-19 | Yunimatekku Kk | 含フッ素カルボン酸の回収方法 |
JP5163125B2 (ja) * | 2005-10-14 | 2013-03-13 | 旭硝子株式会社 | 塩基性陰イオン交換樹脂の再生方法 |
JP2007283224A (ja) * | 2006-04-18 | 2007-11-01 | Asahi Glass Co Ltd | 含フッ素乳化剤の回収方法 |
WO2009157416A1 (ja) | 2008-06-24 | 2009-12-30 | 旭硝子株式会社 | 含フッ素化合物の精製方法 |
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Also Published As
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US7351342B2 (en) | 2008-04-01 |
AU2003244295A1 (en) | 2004-01-06 |
CN100381366C (zh) | 2008-04-16 |
RU2315718C2 (ru) | 2008-01-27 |
DE60304469D1 (de) | 2006-05-18 |
AU2003244295A8 (en) | 2004-01-06 |
US20050150833A1 (en) | 2005-07-14 |
EP1514848B1 (en) | 2006-04-05 |
JPWO2004000734A1 (ja) | 2005-10-20 |
CN1662451A (zh) | 2005-08-31 |
RU2005101086A (ru) | 2005-06-27 |
DE60304469T2 (de) | 2006-11-23 |
EP1514848A8 (en) | 2006-03-01 |
JP4455327B2 (ja) | 2010-04-21 |
EP1514848A1 (en) | 2005-03-16 |
EP1514848A4 (en) | 2005-08-31 |
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