WO2002002669A1 - Verbessertes verfahren zur einstufigen herstellung von polytetrahydrofuran und tetrahydrofuran-copolymeren - Google Patents
Verbessertes verfahren zur einstufigen herstellung von polytetrahydrofuran und tetrahydrofuran-copolymeren Download PDFInfo
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- WO2002002669A1 WO2002002669A1 PCT/EP2001/007427 EP0107427W WO0202669A1 WO 2002002669 A1 WO2002002669 A1 WO 2002002669A1 EP 0107427 W EP0107427 W EP 0107427W WO 0202669 A1 WO0202669 A1 WO 0202669A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/30—Post-polymerisation treatment, e.g. recovery, purification, drying
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/04—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers only
- C08G65/06—Cyclic ethers having no atoms other than carbon and hydrogen outside the ring
- C08G65/16—Cyclic ethers having four or more ring atoms
- C08G65/20—Tetrahydrofuran
Definitions
- the invention relates to a process for the preparation of polytetrahydrofuran or tetrahydrofuran copolymers by polymerizing tetrahydrofuran over an acidic, heterogeneous catalyst in the presence of at least one telogen and / or comonomer selected from alpha, omega-diols, water, polytetrahydrofuran of average molecular weight from 200 to 700 daltons and / or cyclic ethers with recycling at least a portion of the unreacted tetrahydrofuran.
- PTHF Polytetrahydrofuran - hereinafter referred to as polyoxybutylene glycol
- PTHF Polytetrahydrofuran
- plastics and synthetic fiber industry as a versatile intermediate and is used, among other things, for the production of polyurethane, polyester and polyamide elastomers.
- PTHF Polytetrahydrofuran
- it is a valuable auxiliary in many application fields, for example as a dispersing agent or when decolorizing (deinking) waste paper.
- PTHF is usually produced industrially by polymerizing tetrahydrofuran - hereinafter referred to as THF for short - on suitable catalysts.
- the chain length of the polymer chains can be controlled by adding suitable reagents and the average molecular weight can thus be set to the desired value. The control is done by selecting the type and amount of the telogen.
- reagents are called chain termination reagents or "telogens”. By choosing suitable telogens, additional functional groups can be introduced at one or both ends of the polymer chain.
- telogens For example, by using carboxylic acids or carboxylic anhydrides as telogens, the mono- or diesters of PTHF can be produced, which then have to be converted to PTHF by saponification or transesterification. These processes are therefore known as two-stage PTHF processes.
- telogens not only act as chain termination reagents, but are also incorporated into the growing polymer chain of the PTHF. They not only have the function of a telogen, but are also a comonomer and can therefore be called both telogens and comonomers with the same authorization.
- comonomers are telogens with two hydroxyl groups like the diols (dialcohols). These can be, for example, ethylene glycol, propylene glycol, butylene glycol, 1, 3-propanediol, 1, -butanediol, 2-butyn-1, 4-diol, 1, 6-hexanediol or low molecular weight PTHF.
- Cyclic ethers such as 1,2-alkylene oxides, for example ethylene oxide or propylene oxide, 2-methyltetrahydrofuran or 3-methyltetrahydrofuran, are also suitable as comonomers.
- 1,2-alkylene oxides for example ethylene oxide or propylene oxide
- 2-methyltetrahydrofuran or 3-methyltetrahydrofuran are also suitable as comonomers.
- comonomers With the exception of water, 1,4-butanediol and low molecular weight PTHF, the use of such comonomers leads to the preparation of tetrahydrofuran copolymers - hereinafter referred to as THF copolymers - and in this way makes it possible to chemically modify PTHF.
- tetrahydrofuran z. B polymerized in the presence of fluorosulfonic acid to polytetrahydrofuran esters and then hydrolyzed to polytetrahydrofuran. Furthermore, tetrahydrofuran z. B. polymerized with acetic anhydride in the presence of acidic catalysts to polytetrahydrofuran diacetate and then z. B. transesterified with methanol to polytetrahydrofuran.
- a disadvantage of such processes is that two-stage work is required and that by-products such as. B. hydrofluoric acid and methyl acetate.
- the one-step synthesis of PTHF is carried out by THF polymerization with water, 1,4-butanediol or low molecular weight PTHF as a telogen on acidic catalysts.
- PTHF trifluoride
- Both homogeneous systems dissolved in the reaction system and heterogeneous, that is to say largely undissolved, systems are known as catalysts.
- EP-B-126 471 describes water-containing heteropolyacids, such as, for example, tungstophosphoric acid for single-stage PTHF synthesis with water as telogen
- EP-B-158 229 discloses the same catalysts for single-stage PTHF synthesis with diols such as 1,4-butanediol as homogeneous catalysts.
- two liquid phases form, a catalyst-containing phase in which, in addition to THF, the majority of the heteropolyacid and water are found, and an organic phase which mainly contains THF, PTHF and residual amounts of the catalyst. Since the removal of the homogeneous catalyst is complex, the heterogeneously catalyzed processes for single-stage PTHF synthesis and for the direct synthesis of THF copolymers have gained in importance.
- PTHF can be produced from THF and water with the aid of super acidic Nafion® ion exchange resins.
- DE-A 44 33 606 describes, inter alia, a process for the preparation of PTHF, by the polymerization of tetrahydrofuran over a heterogeneous catalyst in the presence of one of the telogens, water, 1,4-butanediol, PTHF having a molecular weight of 200 to 5,700 daltons or mixtures thereof Telogens, the catalyst being a supported catalyst which contains a catalytically active amount of an oxygen-containing tungsten or molybdenum compound or mixtures of these compounds on an oxidic support material and after application of the precursor compounds of the oxygen-containing molybdenum and / or tungsten compounds from 500 ° C. to 1000 ° C has been calcined. From DE-A 196 49 803 it is known / to increase the activity of the catalysts described in DE-A 44
- Polytetrahydrofuran and THF copolymer sales products must have a certain average molecular weight, predominantly in the range between 650 and 5000 daltons, and a narrow molecular weight distribution. At the same time, they must not exceed certain color number limits. The color number must be below 40, preferably below 20 APHA. 5
- a disadvantage of the known homogeneously or heterogeneously catalyzed processes for the single-stage synthesis of PTHF or of THF copolymers is that not all of the above-mentioned properties of the PTHF and / or the THF copolymers required for the sales products are realized at the same time to let.
- Numerous post-treatment processes for cleaning and reducing the color number of the PTHFs and / or the THF copolymers are known, in which the products obtained from the polymerization, for example as in EP-A 424 791, are post-treated with hydrogen in the presence of a hydrogenation catalyst become.
- the object of the present invention was to find an economical, one-step process which makes it possible to obtain both PTHF and THF copolymers with a narrow molecular weight distribution and a low color number in a high space-time yield and with high selectivity.
- At least one distillation stage is separated into a distillation residue containing the polymerization product and at least one tetrahydrofuran fraction is carried out and the tetrahydrofuran fraction is at least partially returned to the polymerization and
- the process according to the invention for the one-step synthesis of PTHF and THF copolymers makes it possible to obtain both PTHF and THF copolymers with a narrow molecular weight distribution and a low color number in a high space-time yield and with high selectivity without a separate aftertreatment process.
- the recycling of the separated tetrahydrofuran contributes to the economy of the process according to the invention.
- a polymerization product is first obtained by cationic polymerization of tetrahydrofuran over an acidic heterogeneous catalyst in the presence of at least one telogen and / or copolymer from the group of alpha, omega-diols, water, polytetrahydrofuran with a molecular weight of 200 to 700 daltons and / or cyclic Made of ethers.
- Acid heterogeneous catalysts are preferably used as polymerization catalysts, the acid centers of the acid strength Ho ⁇ +2 in a concentration of at least 0.005 mmol / g catalyst, particularly preferably an acid strength H 0 ⁇ +1.5 in a concentration of at least 0.01 mmol / g catalyst.
- sulfonated zirconium dioxide can be used as polymerization catalysts, alpha- Polymers containing fluorosulfonic acids, supported catalysts made of an oxidic support material, which contain a catalytically active amount of a tungsten or molybdenum compound or mixtures of such compounds, are used, supported catalysts made of an oxidic support material containing a catalytically active amount of a tungsten or molybdenum compound or mixtures contain such compounds, are preferred.
- Sulphate-doped zirconium dioxide which is suitable for the process according to the invention can be produced, for example, by the process described in US Pat. No. 5,149,862.
- polymers containing alpha-fluorosulfonic acid can also be used as the polymerization catalyst.
- polymers containing perfluorinated alpha-fluorosulfonic acid which are marketed, for example, under the name Nafion by E.I. du Pont de Nemours and Company are sold as a commercial product.
- Suitable supported catalysts made of an oxidic support material which contain oxygen-containing molybdenum or tungsten compounds or mixtures of such compounds as catalytically active compounds and which, if desired, can also be additionally doped with sulfate or phosphate groups are described in DE-A 44 33 606, to which explicit reference is made here. As in DE 19641481, which is expressly referred to here, these catalysts can be pretreated with a reducing agent, preferably with hydrogen.
- the supported catalysts described in German patent application DE 19649803, to which reference is expressly made here are suitable which contain as the active composition a catalytically active amount of at least one oxygen-containing molybdenum and / or tungsten compound and which, after preparation of the precursor compounds of the active composition, on the support material - Precursors have been calcined at temperatures from 500 ° C to 1000 ° C, which contain a promoter, which includes at least one element or a compound of an element of the 2nd, 3rd - loaned the anthanids, 5th, 6th, 7th , 8th or 14th group of the Periodic Table of the Elements.
- These catalysts generally contain 0.01 to 30% by weight, preferably 0.05 to 20% by weight and particularly preferably 0.1 to 15% by weight, of the promoter, calculated as the sum of its constituents in the form of their elements and based on the total weight of the catalyst.
- the catalysts which can be used according to the invention and are known from DE-A 44 33 606 and DE 196 49 803 generally contain 0.1 to 50% by weight of the catalytically active, oxygen-containing compounds of molybdenum or tungsten or the mixtures of the catalytically active, oxygen-containing compounds of these metals, in each case based on the total weight of the catalyst and since the chemical structure of the catalytically active, oxygen-containing compounds of molybdenum and / or tungsten has not hitherto been known exactly, calculated in each case as M0O 3 or WO 3 .
- catalysts which can be used according to the invention and which contain at least one catalytically active, oxygen-containing molybdenum and / or tungsten compound on an oxidic support and which after application of the Precursor compounds of the catalytically active compounds on the support material or a support material precursor have been calcined at temperatures of 400 ° C. to 900 ° C., which have a porosity of the catalyst with transport pores each having a diameter of ⁇ 25 ⁇ m and a volume of these transport pores of at least 50 mm 3 / g.
- the catalysts described in these two parallel applications contain 0.1 to 70% by weight, preferably 5 to 40% by weight and particularly preferably 10 to 35% by weight of the catalytically active oxygen-containing molybdenum and / or tungsten compound ( en), calculated as M0O 3 and / or WO 3 and based on the total weight of the catalyst.
- Suitable oxidic supports for the oxygen-containing molybdenum or tungsten compounds or mixtures of such compounds as catalysts containing catalytically active compounds are, for example, zirconium dioxide, titanium dioxide, hafnium oxide, yttrium oxide, iron (III) oxide, aluminum oxide, tin (IV) oxide, silicon dioxide, zinc oxide or mixtures of these oxides.
- zirconium dioxide, titanium dioxide and / or silicon dioxide are particularly preferred, and titanium dioxide is particularly preferred.
- phyllosilicates or zeolites activated by acid treatment can, if desired, be used as heterogeneous catalysts in the process according to the invention.
- Layered silicates which are preferred are those of the montmorillonite-saponite, kaolin-serpentine or palygorskite-sepiolite group, particularly preferably montmorillonite, hectorite, kaolin, attapulgite or sepiolite, as described, for example, in Klockmann's textbook on mineralogy, 16th edition , F. Euke Verlag 1978, pages 739-765.
- Montmorillonite can be used as under the name Tonsil ®, Terrana ® or Granosil ® or as catalysts of the types Tonsil ® K 10, KSF-0, KO or KS in Sud-Chemie AG, Kunststoff, are available.
- Attasorb ® RVM and LVM Attasorb ® proper procedure appropriate Attapulgite example by Engelhard Corporation, Iselin, USA, - for use in the fiction,.
- Zeolites are a class of aluminum hydrosilicates that, due to their special chemical structure in the crystal, form three-dimensional networks with defined pores and channels. Natural or synthetic zeolites are suitable for the inventive method, said zeolites having a SiO 2 -Al 2 ⁇ 3 molar ratio of 4: 1 is preferred, with a SiO 2 -Al 2 ⁇ 3 molar ratio of 6: 1 to 100 1 to 90 1 are particularly preferred: 1 and more preferably having a SiO 2 -Al 2 ⁇ 3 molar ratio of 10: 1 to 80 wt.
- the primary crystallites of these zeolites preferably have a particle size of up to 0.5 ⁇ m, preferably 0.1 ⁇ m and particularly preferably 0.05 ⁇ m.
- the zeolites which can be used in the process according to the invention are used in the so-called H form. This is characterized in that azide OH groups are present in the zeolite. If the zeolites are not already produced in H form during their production, they can easily be broken down by acid treatment with, for example, mineral acids such as hydrochloric acid, sulfuric acid, phosphoric acid or by thermal treatment of suitable precursor zeolites which contain, for example, ammonium ions, for example by heating Temperatures of 450 to 600 ° C, preferably 500 to 550 ° C, are converted into the catalytically active H form.
- mineral acids such as hydrochloric acid, sulfuric acid, phosphoric acid
- suitable precursor zeolites which contain, for example, ammonium ions
- heterogeneous catalysts which can be used according to the invention can be in the form of powder, for example when carrying out the process in suspension mode, or expediently as shaped articles, for example in the form of cylinders, balls, rings, spirals or 5 chips, in particular in the case of a fixed bed arrangement of the catalyst, in the process according to the invention are used, the use as a shaped body in a fixed bed being preferred.
- THF can in principle be used as the monomer 10.
- Suitable telogens and / or comonomers in the process according to the invention are saturated or unsaturated, unbranched or branched alpha, omega-C 2 to C 2 -diols, water, polytetrahydrofuran with a molecular weight of 200 to 700 daltons, cyclic ethers or their mixtures.
- telogens for the production of PTHF and THF copolymers
- 8-octanediol 1,10-decanediol, 2-butyn-l, 4-diol and neopentyl glycol or mixtures thereof
- Cyclic ethers which can be polymerized to open the ring, preferably three-membered, four-membered and five-membered rings such as 1,2-alkylene oxides, for example ethylene oxide, are suitable as comonomers
- oxetane substituted oxetanes such as 3,3-dimethyloxetane
- the THF derivatives 2-methyltetrahydrofuran or 3-methyltetrahydrofuran suitable, 2-methyltetrahydrofuran or 3-methyltetrahydrofuran being particularly preferred.
- telogen is expediently fed to the polymerization in solution in the THF, a telogen content of 0.04 to 17 mol%, based on tetrahydrofuran, being preferred.
- Comonomers are also expediently fed to the polymerization in solution in THF, the comonomer content up to 30 mol%, preferably
- Control 45 of the THF copolymers The more telogen the reaction mixture contains, the lower the average molecular weight of the PTHF or the THF copolymers in question. Depending on the telogen content of the polymerization mixture, PTHF and THF copolymers with average molecular weights of 650 to 5000 Daltons, preferably from 650 to 3000 Daltons and particularly preferably from 1000 to 3000 Daltons can be produced.
- the polymerization is generally carried out at temperatures from 0 to 80 ° C., preferably at 25 to 75 ° C., and particularly preferably at 40 to 70 ° C.
- the pressure used is generally not critical to the result of the polymerization, which is why work is generally carried out at atmospheric pressure or under the autogenous pressure of the polymerization system.
- the polymerization is advantageously carried out under an inert gas atmosphere.
- inert gases e.g. Nitrogen, carbon dioxide or the noble gases are used, nitrogen is preferably used.
- the polymerization can also be carried out in the presence of hydrogen at hydrogen pressures of 0.1 to 10 bar.
- the process according to the invention is preferably operated continuously with all of its stages. However, it is also possible to operate the polymerization stage and / or one, more or all of the work-up stages of the process according to the invention batchwise, but preferably at least the polymerization is carried out continuously.
- the reaction can be carried out in conventional reactors or reactor arrangements suitable for continuous processes in suspension or fixed bed mode, for example in loop reactors or stirred reactors in suspension mode or in fixed bed mode in tubular reactors or fixed bed reactors, the fixed bed mode being preferred.
- the catalyst can, if desired, be pretreated after it has been introduced into the reactor.
- Pre-treatment of the catalyst is, for example, drying with gases heated to 80-200 ° C., preferably 100 to 150 ° C., such as air or nitrogen, or pre-treatment with a reducing agent, as described in DE 196 41 481 for the invention preferred supported catalysts, which contain a catalytically active amount of at least one oxygen-containing molybdenum and / or tungsten compound, are described as the active composition.
- gases heated to 80-200 ° C. preferably 100 to 150 ° C., such as air or nitrogen
- pre-treatment with a reducing agent as described in DE 196 41 481 for the invention preferred supported catalysts, which contain a catalytically active amount of at least one oxygen-containing molybdenum and / or tungsten compound, are described as the active composition.
- the catalyst can also be used without pretreatment.
- the polymerization reactor can be operated in a bottom mode, ie the reaction mixture is conducted from bottom to top, or in a trickle mode, ie the reaction mixture is passed through the reactor from top to bottom.
- the starting material mixture (feed) of THF and telogen and / or comonomer is fed continuously to the polymerization reactor, the catalyst loading being 0.05 to 0.8 kg THF / (lh), preferably 0.1 to 0.6 kg THF / (lh) and particularly preferably 0.15 to 0.5 kg THF / (lh).
- the polymerization reactor can be operated in a single pass, that is to say without product recirculation, or in circulation, that is to say the polymerization mixture leaving the reactor is operated in a circuit.
- the ratio of circulation to inlet is less than or equal to 100: 1, preferably less than 50: 1 and particularly preferably less than 40: 1.
- the concentration of the alpha, omega-diol, water, polytetrahydrofuran with an average molecular weight of 200 to 700 daltons or of their mixture in the feed mixture (feed) fed to the polymerization reactor is between 0.02 and 20 mol%, preferably 0, 05 to 15 mol%, particularly preferably 0.1 to 10 mol%, based on the THF used.
- the polymerization discharge is fed directly to processing stage a).
- the suspended and / or dissolved catalyst fractions and / or catalyst secondary products separated in workup stage a) are, for example, finely divided, suspended or emulsified catalyst abrasion, which consists of unchanged catalyst, the catalyst support and / or the catalyst active component consists.
- the catalyst is unchanged, carrier components and / or the oxygen-containing molybdenum or tungsten active components.
- catalyst secondary products are, for example, dissolved cations or anions of the active components, such as. B.
- sulfonic acid-containing ion exchangers such as Nafion ® may be fluoride ions and / or sulfonic acids
- sulfate-doped metal oxides to sulfuric acid and / or metal cations or anions act.
- the catalyst fractions and / or catalyst secondary products can be separated off from the polymerization discharge by filtration, such as, for example, ultrafiltration, adsorption on solid adsorbents and / or with the aid of ion exchangers, filtration and adsorption on solid adsorbents being preferred.
- filtration such as, for example, ultrafiltration, adsorption on solid adsorbents and / or with the aid of ion exchangers, filtration and adsorption on solid adsorbents being preferred.
- the adsorption on the solid adsorbent mentioned can also be combined with a neutralization of the polymerization output with acids or bases.
- the adsorption is preferably carried out on activated carbon and / or metal oxides and / or ion exchangers at temperatures of 25 to 75 ° C., preferably at 30 ° C. to 70 ° C.
- the separation in processing stage a) is particularly preferably carried out on ion exchangers and / or activated carbon.
- the preferred metal oxides are sodium hydroxide, aluminum oxide, silicon dioxide, titanium dioxide, zirconium dioxide, lanthanum oxide and / or calcium oxide use.
- Suitable activated carbon can be obtained, for example, from Merck, Darmstadt or in the form of the commercial product activated carbon type CPG UF 8x30 from Chemviron Carbon.
- Suitable ion exchangers are, for example, anion exchangers such as the commercial product Lewatit MP 600, which can be obtained from Bayer AG, Leverkusen, and mixed ion exchangers, such as the commercial product Serdolit®, which is available from Serva,
- the inventive separation of the catalyst fractions and / or catalyst secondary products by adsorption on solid adsorbents is preferred in a fixed bed at a load of generally 0.2 to 5 kg / (l * h), in particular 0.4 to 4 kg / ( l * h) (kg of polymer discharge per 1 adsorbent per hour) used.
- the processing stage b) can be operated batchwise or continuously, preferably continuously. It serves for the extensive to complete separation of the unreacted tetrahydrofuran from PTHF or from the THF copolymers by distillation.
- the THF removal in the work-up stage b) can in principle be carried out in one distillation stage, but preferably in several, preferably two or three, stages, it being advantageous to work at different pressures.
- the design of work-up stage b) of the process according to the invention depends on the telogen used in the polymerization.
- suitable columns or evaporators such as e.g. Falling film evaporators or thin film evaporators in question. Separating plate columns can also advantageously be used.
- stage b) Possible processing variants of stage b) for the use of THF and water as telogen in the polymerization are explained in more detail below.
- the main amount of unreacted THF is separated off at atmospheric pressure in a continuously operated distillation column.
- the catalyst-free polymerization discharge obtained with water as telogen in processing stage a) which has a polymer content of usually 2 to 25% and Water content of max.
- a head temperature of 66 to 67 ° C and a bottom temperature of 100 to 200 ° C, preferably 120 to 180 ° C the majority of water in a mixture with tetrahydrofuran is distilled off overhead.
- the tetrahydrofuran fraction obtained as a distillate is condensed and then wholly or partly returned to the polymerization.
- the THF / PTHF mixture obtained in the bottom of the column as a distillation residue contains, depending on the selected bottom temperature, about 2 to 20% by weight of THF and usually up to max. approx. 300 ppm water, each based on the THF / PTHF mixture.
- the main amount of unreacted THF can also be separated off at atmospheric pressure in a thin-film evaporator, preferably in a falling-film evaporator with circulation, which is operated at 100 to 200 ° C., preferably 120-180 ° C.
- the composition of the tetrahydrofuran fraction obtained as a distillate and of the THF / PTHF mixture obtained as a distillation residue corresponds to that described above.
- the distillation residue obtained from the first distillation stage is then largely completely freed of residual amounts of tetrahydrofuran in a falling film evaporator at 120 to 160 ° C., in particular approx. 130 ° C. and 50 to 200 rabar, in particular 70 to 150 mbar ,
- the THF fraction obtained as a distillate, which mainly consists of THF, can be wholly or partly returned to the polymerization.
- stage b For the use of THF and diols as telogens in the polymerization, the following processing variants of stage b) are possible. It was recognized according to the invention that the water content of the polymerization discharge when using diols as telogens in the polymerization is usually higher than the water content of the feed. In the reprocessing variants, discharge options for water are therefore taken into account.
- the removal of the main amount of unreacted THF at normal pressure and removal of the main amount of water can be carried out in a continuously operated distillation column, preferably in a separating plate column.
- the catalyst-free polymerization output obtained with diols as telogens in processing stage a), which has a polymer content of usually 2 to 25% and water contents of max. contains about 500 ppm, fed into a distillation column via a side inlet.
- a head temperature of approx. 66 to 67 ° C and a bottom temperature of 100 to 200 ° C, preferably 120 to 180 ° C the catalyst-free polymerization discharge is separated in the column into a THF / water mixture as top product, which contains the main amount of water in a concentration of max.
- a THF fraction which contains the main amount of THF, is largely anhydrous and generally contains less than 100 ppm, preferably ⁇ 50 ppm water, and can therefore be wholly or partly recycled into the polymerization.
- the distillation residue in the bottom of the column is a THF / PTHF mixture which, depending on the bottom temperature selected, contains about 2 to 20% by weight of THF and a water content of max. has about 100 ppm.
- the bulk of the unreacted can be separated.
- THF at normal pressure can also be carried out in a thin-film evaporator, preferably in a falling-film evaporator with circulation, which is operated at 100 to 200 ° C., preferably 120-180 ° C.
- the catalyst-free polymerization output obtained under a) is separated into a water-containing THF fraction as the distillate and a THF / diol / PTHF mixture as the distillation residue.
- the water-containing THF fraction can then in a distillation column preferably at normal pressure and at about 63 to 65 ° C top temperature and about 70 ° C bottom temperature in a THF / water mixture with a max. Water content of approx. 5% as distillate and a largely anhydrous tetrahydrofuran fraction as distillation residue, as bottom or side draw from the column. This largely anhydrous THF fraction can be wholly or partly returned to the polymerization.
- the THF / diol / PTHF mixture obtained as the distillation residue after the respective first distillation stage is then preferably in vacuo in a falling film evaporator at 120 to 160 ° C., in particular approximately 130 ° C. and 50 to 200 mbar, in particular 70 to 150 mbar largely completely freed from residual amounts of tetrahydrofuran.
- the THF fraction obtained as a distillate which mainly consists of THF and, depending on the vapor pressure of the diols used, may still have small amounts of diol, can be recycled in whole or in part into the polymerization.
- distillation residue from work-up stage b) before the transfer to work-up stage c) with alkanes, such as, for example, pentane, hexane, heptane or octane, as described in EP-A 153 794, by the content of to reduce cyclic oligomers.
- alkanes such as, for example, pentane, hexane, heptane or octane, as described in EP-A 153 794
- processing stage c) the distillation residue from processing stage b) is then converted into at least one further distillation stage at a pressure of 0.1 to 50 mbar, preferably 0.1 to 10 mbar, particularly preferably 0.1 to 5 mbar, and a 5th Temperature of 180 to 280 ° C, preferably 200 to 250 ° C, particularly preferably 230 to 250 ° C low molecular weight polytetrahydrofuran or low molecular weight tetrahydrofuran copolymers of an average molecular weight of 200 to 700 daltons separated and polytetrahydrofuran or tetrahydrofuran copolymers of an average
- telogens 10 molecular weight from 650 to 5000 daltons.
- diols used as telogens are almost completely distilled off from the product of value under the distillation conditions.
- Simple evaporators such as thin-film evaporators, falling-film evaporators or short-path evaporators, can be used as distillation apparatus.
- the low molecular weight polytetrahydrofuran and / or tetrahydrofuran copolymer of an average molecular weight of 200 to 700 daltons containing distillate of workup stage c) can, if desired, be wholly or partly fed into the polymerization.
- PTHF and / or the THF copolymers with average molecular weights of 25,650 to 5,000 daltons are obtained as the distillation residue of work-up stage c).
- Figure 1 shows a schematic representation of the implementation of the method according to the invention.
- the average molecular weight (M n ) of the PTHF obtained was determined by gel permeation chromatography (GPC) and is defined by the equation
- Mw and Mn were determined by GPC using a standardized PTHF for calibration.
- the number average M n according to the equation was obtained from the chromatograms obtained
- ci stands for the concentration of the individual polymer species i in the polymer mixture obtained and in Mi means the molecular weight of the individual polymer species i.
- the catalyst was prepared by adding 124.7 kg of titanium dioxide (water content of 23.3% by weight), 25.5 kg of tungstic acid (H 2 WO 4 ) and 6.0 kg of tartaric acid to a solution of 146 kg of 87% Phosphoric acid (H 3 PO 4 ) in 45.5 kg water. This mixture was rolled for 0.5 hours, extruded into strands 4.5 mm in diameter and dried at 120 ° C. for 2 hours. The catalyst was then calcined at 690 ° C. for 3 hours. The catalyst had a tungsten content, calculated as wolf amtrioxide, of 20% by weight based on the total weight of the catalyst.
- 1,4-butanediol-containing THF (feed) per hour were passed continuously over 28 kg of the W 3 / Ti O 2 catalyst prepared according to Example 1, which was arranged as a fixed bed in a 30 1-tube reactor ,
- the feed contained 0.36% by weight of 1,4-butanediol, corresponding to a 1,4-butanediol supply of 25 g / h, and approximately 40 ppm of water.
- the reactor was operated in circulation mode with a circulation at a circulation / feed ratio of 100: 1.
- the reaction discharge of the polymerization reactor was passed at 60 ° C and a load of 2.8 kg feed / (1 * h) over activated carbon (Che viron Carbon; type CPG UF 8 x 30), which was in a 2.5 1 container Fixed bed was arranged.
- the activated carbon-treated mixture was then passed into a distillation column with 32 theoretical plates via a side inlet. At a bottom temperature of 115 ° C. and a pressure of 1100 mbar, 0.08 kg of a THF / water mixture with a water content of approx. 2% by weight was separated off at the top of the column.
- Example 2 The reaction conditions of Example 2 were maintained, but the amount of butanediol fed per hour in the polymerization was reduced from 25 g to 21.9 g. After working up the polymerization discharge as described in Example 2, PTHF with an average molecular weight M n 2900, a dispersity D of 2.3 and a color number of 5 APHA were obtained. The space-time yield was 18.6 g of PTHF 2900 / (1 * h), the THF conversion was 7.8%.
- Example 4 Example 4
- Example 2 The conditions of Example 2 were maintained, but the amount of butanediol recycled per hour was increased to 27 g. After working up the polymerization discharge as described in Example 2, PTHF with an average molecular weight Mn 1810, a dispersity D of 1.9 and a color number of 6 APHA were obtained. The space-time yield achieved was 10.3 g of PTHF 1810 / (1 * h), the THF conversion was 4.0%.
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Abstract
Description
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Priority Applications (4)
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JP2002507918A JP2004502806A (ja) | 2000-07-03 | 2001-06-29 | ポリテトラヒドロフランおよびテトラヒドロフラン−コポリマーを1工程で製造するための改善された方法 |
KR10-2003-7000013A KR20030016366A (ko) | 2000-07-03 | 2001-06-29 | 폴리테트라하이드로푸란 및 테트라하이드로푸란코폴리머의 일단계 제조를 위한 개선된 방법 |
US10/312,851 US6716937B2 (en) | 2000-07-03 | 2001-06-29 | Method for the single-step production of polytetrahydrofuran and tetrahydrofuran copolymers |
EP01945325A EP1299449A1 (de) | 2000-07-03 | 2001-06-29 | Verbessertes verfahren zur einstufigen herstellung von polytetrahydrofuran und tetrahydrofuran-copolymeren |
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DE10032266.2 | 2000-07-03 | ||
DE10032266A DE10032266A1 (de) | 2000-07-03 | 2000-07-03 | Verbessertes Verfahren zur einstufigen Herstellung von Polytetrahydrofuran und Tetrahydrofuran-Copolymeren |
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PCT/EP2001/007427 WO2002002669A1 (de) | 2000-07-03 | 2001-06-29 | Verbessertes verfahren zur einstufigen herstellung von polytetrahydrofuran und tetrahydrofuran-copolymeren |
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US (1) | US6716937B2 (de) |
EP (1) | EP1299449A1 (de) |
JP (1) | JP2004502806A (de) |
KR (1) | KR20030016366A (de) |
CN (1) | CN1440437A (de) |
DE (1) | DE10032266A1 (de) |
WO (1) | WO2002002669A1 (de) |
Cited By (3)
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WO2002072666A1 (de) * | 2001-03-14 | 2002-09-19 | Basf Aktiengesellschaft | Verfahren zur herstellung von polyetherolen mit definiertem cpr-wert |
EP1433807A1 (de) * | 2002-12-20 | 2004-06-30 | Hodogaya Chemical Co Ltd | Verfahren zur Herstellung von Polyetherpolyolen mit enger Molekulargewichtsverteilung |
US7276573B2 (en) * | 2002-09-12 | 2007-10-02 | Basf Aktiengesellschaft | Method for producing monoesters and diesters of polytetrahydrofuran and of tetrahydrofuran copolymers |
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DE10261484A1 (de) | 2002-12-23 | 2004-07-01 | Basf Ag | Verfahren zur Polymerisation cyclischer Ether |
DE10330721A1 (de) * | 2003-07-08 | 2005-01-27 | Basf Ag | Verfahren zur Gewinnung von Oligomeren des Polytetrahydrofurans oder der Tetrahydrofuran-Copolymere |
DE10359808A1 (de) * | 2003-12-19 | 2005-07-21 | Basf Ag | Verfahren zur Herstellung von Tetrahydrofuran-Copolymeren |
WO2008086919A1 (de) * | 2007-01-19 | 2008-07-24 | Basf Se | Verfahren zur änderung des vorgegebenen mittleren molekulargewicht mn bei der kontinuierlichen herstellung von polytetrahydrofuranen oder thf copolymeren |
KR100914059B1 (ko) * | 2007-11-26 | 2009-08-28 | 주식회사 효성 | 테트라하이드로푸란 중합체의 제조 방법 |
US20100267905A1 (en) * | 2009-04-15 | 2010-10-21 | Invista North America S.A R.L. | Copolyether glycol manufacturing process |
KR20120017040A (ko) * | 2009-04-15 | 2012-02-27 | 인비스타 테크놀러지스 에스.에이.알.엘. | 코폴리에테르 글리콜 제조 방법 |
US8609805B2 (en) | 2009-04-15 | 2013-12-17 | Invista North America S.A R.L. | Copolyether glycol manufacturing process |
CN102923387A (zh) * | 2011-08-10 | 2013-02-13 | 因温斯特技术公司 | 用于聚醚多元醇产品的颜色管理 |
US20150158976A1 (en) | 2012-06-22 | 2015-06-11 | Invista North America S.A.R.L. | Alkanolysis process and method for separating catalyst from product mixture |
CN103890068A (zh) * | 2012-07-02 | 2014-06-25 | 因温斯特北美公司 | 四氢呋喃清洗处理方法 |
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TW201529636A (zh) | 2013-12-19 | 2015-08-01 | Invista Tech Sarl | 經改良的聚四亞甲基醚二醇製造方法 |
CN103755944B (zh) * | 2014-01-10 | 2015-12-02 | 大连工业大学 | 复合金属氧化物修饰二氧化钛型固体酸的制备方法及其催化聚四氢呋喃醚的合成方法 |
CN115725066A (zh) * | 2022-11-15 | 2023-03-03 | 河南省生物基材料产业研究院有限公司 | 一种生物基聚四氢呋喃的制备方法 |
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-
2000
- 2000-07-03 DE DE10032266A patent/DE10032266A1/de not_active Withdrawn
-
2001
- 2001-06-29 EP EP01945325A patent/EP1299449A1/de not_active Withdrawn
- 2001-06-29 JP JP2002507918A patent/JP2004502806A/ja not_active Withdrawn
- 2001-06-29 CN CN01812293A patent/CN1440437A/zh active Pending
- 2001-06-29 WO PCT/EP2001/007427 patent/WO2002002669A1/de not_active Application Discontinuation
- 2001-06-29 US US10/312,851 patent/US6716937B2/en not_active Expired - Fee Related
- 2001-06-29 KR KR10-2003-7000013A patent/KR20030016366A/ko not_active Application Discontinuation
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WO2002072666A1 (de) * | 2001-03-14 | 2002-09-19 | Basf Aktiengesellschaft | Verfahren zur herstellung von polyetherolen mit definiertem cpr-wert |
US7276573B2 (en) * | 2002-09-12 | 2007-10-02 | Basf Aktiengesellschaft | Method for producing monoesters and diesters of polytetrahydrofuran and of tetrahydrofuran copolymers |
EP1433807A1 (de) * | 2002-12-20 | 2004-06-30 | Hodogaya Chemical Co Ltd | Verfahren zur Herstellung von Polyetherpolyolen mit enger Molekulargewichtsverteilung |
US8053607B2 (en) | 2002-12-20 | 2011-11-08 | Hodogaya Chemical Co., Ltd. | Method for producing polyether-polyol having narrow molecular weight distribution |
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US20030176630A1 (en) | 2003-09-18 |
JP2004502806A (ja) | 2004-01-29 |
DE10032266A1 (de) | 2002-01-17 |
KR20030016366A (ko) | 2003-02-26 |
US6716937B2 (en) | 2004-04-06 |
EP1299449A1 (de) | 2003-04-09 |
CN1440437A (zh) | 2003-09-03 |
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