WO2013005749A1 - テトラヒドロフランの製造方法 - Google Patents
テトラヒドロフランの製造方法 Download PDFInfo
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- WO2013005749A1 WO2013005749A1 PCT/JP2012/067012 JP2012067012W WO2013005749A1 WO 2013005749 A1 WO2013005749 A1 WO 2013005749A1 JP 2012067012 W JP2012067012 W JP 2012067012W WO 2013005749 A1 WO2013005749 A1 WO 2013005749A1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B61/00—Other general methods
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- 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
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/002—Processes specially adapted for distillation or rectification of fermented solutions by continuous methods
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- 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
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/04—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
- C07D307/06—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, directly attached to ring carbon atoms
- C07D307/08—Preparation of tetrahydrofuran
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to a method for producing tetrahydrofuran, and more particularly to a method for producing tetrahydrofuran stably and efficiently by dehydration cyclization of 1,4-butanediol using an acid catalyst.
- Tetrahydrofuran (hereinafter sometimes abbreviated as “THF”) is a useful compound as a solvent for various organic compounds including polymer compounds, a raw material for polytetramethylene glycol, and the like.
- Tetrahydrofuran is often produced industrially by a dehydration cyclization reaction of 1,4-butanediol (hereinafter sometimes abbreviated as “1,4BG”).
- 1,4BG 1,4-butanediol
- an acid catalyst is effective in either a homogeneous system or a heterogeneous system.
- Patent Document 1 For example, methods using a solid catalyst such as a silica-alumina catalyst (Patent Document 1) and a cation exchange resin (Patent Document 2) are known. However, these methods have a significant catalyst deterioration under high temperature conditions. There are problems such as. In recent years, a process for producing tetrahydrofuran using a heteropolyacid (Patent Document 3), which is considered to have little catalyst deterioration even under high temperature conditions, has been proposed.
- Patent Document 3 a process for producing tetrahydrofuran using a heteropolyacid
- Patent Document 3 describes that precipitation of by-product solids such as a polymer makes operation difficult, and is a reaction by-product at the time of 1,4BG synthesis, which is a raw material 1,4BG. It describes the production of solids derived from 2- (4-hydroxybutoxy) -tetrahydrofuran (hereinafter sometimes abbreviated as “BGTF”) contained as impurities.
- BGTF 2- (4-hydroxybutoxy) -tetrahydrofuran
- the present invention has been made in view of the above problems, and in producing tetrahydrofuran by a dehydration cyclization reaction using 1,4-butanediol as a raw material in the presence of an acid catalyst, precipitation of by-product solids is performed.
- An object of the present invention is to provide an industrially advantageous method for producing tetrahydrofuran which can be prevented and stably provide high productivity.
- the present inventors have made by-product water present by allowing at least one of a specific amount of amine and amide to be present in 1,4BG used for the production of tetrahydrofuran.
- the amount of 2- (4-hydroxybutoxy) -tetrahydrofuran in the reactor can be reduced to effectively suppress the formation of by-product solids. Even when a raw material 1,4-butanediol containing a certain amount of (4-hydroxybutoxy) -tetrahydrofuran is used, precipitation of by-product solids in the reactor can be prevented and stable high productivity can be maintained. I found out what I can do.
- a method for producing tetrahydrofuran by carrying out a dehydration cyclization reaction of 1,4-butanediol in the presence of an acid catalyst having a pKa value of 4 or less in a reactor The raw material liquid containing 4-butanediol is 0.01 to 0.35% by weight of 2- (4-hydroxybutoxy) -tetrahydrofuran, and at least one of amine and amide is 1 ppm by weight or more in terms of nitrogen atom, 1000 A method for producing tetrahydrofuran, containing not more than ppm by weight.
- [2] A method for producing tetrahydrofuran by carrying out a dehydration cyclization reaction of 1,4-butanediol in the presence of an acid catalyst having a pKa value of 4 or less in the reactor, and the reaction in the reactor
- [3] The process for producing tetrahydrofuran according to [1], wherein the reaction liquid in the reactor contains at least one of amine and amide in a nitrogen atom equivalent concentration of 1 ppm by weight or more and 10,000 ppm by weight or less.
- [4] The method for producing tetrahydrofuran according to any one of [1] to [3], wherein the reaction liquid in the reactor contains water in an amount of 0.1 wt% to 10 wt%.
- [5] The method for producing tetrahydrofuran according to any one of [1] to [4], including a step of extracting a gas containing tetrahydrofuran and water present in a gas phase portion in the reactor to the outside of the reactor.
- [6] The process for producing tetrahydrofuran according to any one of [1] to [5], wherein the temperature of the reaction solution in the reactor is in the range of 80 ° C. or higher and 250 ° C. or lower.
- the present invention in the process for producing tetrahydrofuran by dehydration cyclization reaction in the presence of an acid catalyst using 1,4-butanediol as a raw material, the amount of 2- (4-hydroxybutoxy) -tetrahydrofuran in the reactor Therefore, precipitation of by-product solids can be prevented, and tetrahydrofuran can be produced with high productivity in a stable operation.
- the method for producing tetrahydrofuran of the present invention is a method for producing tetrahydrofuran by carrying out a dehydration cyclization reaction of 1,4-butanediol in a reactor in the presence of an acid catalyst having a pKa value of 4 or less.
- the content of 2- (4-hydroxybutoxy) -tetrahydrofuran in the raw material liquid containing 1,4-butanediol in the reactor at the start of the dehydration cyclization reaction is 0.01 to 0.35% by weight;
- the content of at least one of amine and amide is 1 ppm by weight or more and 1000 ppm by weight or less in terms of nitrogen atom, or at least one of amine and amide in nitrogen atom equivalent concentration in the reaction liquid in the reactor. 1 wt ppm or more and 10,000 wt ppm or less.
- [1,4-butanediol] 1,4BG used in the present invention can be obtained by a known method.
- 1,4-BG can be produced by hydrogenating 1,4-diacetoxy-2-butene obtained by diacetoxylation of butadiene and then hydrolyzing it.
- 1,4BG obtained by hydrogenation of maleic anhydride, 1,4BG derived from acetylene by the Reppe method, 1,4BG obtained by oxidation of propylene, 1,4BG obtained by the fermentation method, etc. are used. You can also.
- 1,4BG produced by such a method is usually BGTF which is a reaction by-product, 1-acetoxy-4-hydroxybutane, dehydrated dimer of 1,4-butanediol, dehydrated trimer, ⁇ -butyrolactone
- BGTF is a reaction by-product, 1-acetoxy-4-hydroxybutane, dehydrated dimer of 1,4-butanediol, dehydrated trimer, ⁇ -butyrolactone
- the content of BGTF is usually 0.01 to 0.5% by weight.
- the raw material 1,4BG supplied to the reactor for the production of THF by the dehydration cyclization reaction is not particularly limited as long as the BGTF concentration in the raw material liquid is within the range described later.
- the content of BGTF in the raw material liquid containing 1,4BG supplied to is 0.01 to 0.35 wt%, preferably 0.10 wt% to 0.33 wt%, more preferably 0.15 % By weight to 0.30% by weight. For this reason, in this invention, it is preferable to supply to a reactor, after performing the process for reducing the BGTF density
- the treatment for reducing the concentration of BGTF in the crude 1,4BG is not particularly limited, and a normal separation operation such as distillation can be adopted.
- the crude 1,4BG is dissolved in the presence of amine and water.
- a method of heating to a temperature of at least ° C is preferred. That is, when crude 1,4BG is heated in the presence of amine and water, BGTF is converted to 2-hydroxytetrahydrofuran or its ring-opening product, 4-hydroxybutyraldehyde or a derivative thereof.
- 2-hydroxytetrahydrofuran does not inhibit the dehydration cyclization reaction, does not cause the formation of by-product solids, and after the dehydration cyclization reaction, 1,4BG is obtained by distillation or the like. And can be easily separated from THF.
- 2-hydroxytetrahydrofuran can be converted to 1,4-butanediol by hydrogenation.
- the method for allowing at least one of amine and amide to be present in crude 1,4BG is not particularly limited, but preferably, crude 1,4BG and an amine system represented by the following formula (1)
- An anion exchange method having a polyamine skeleton, a method of mixing a compound and its decomposition product, one or more selected from the amide represented by the following formula (2) and its decomposition product, or a crude 1,4BG A method of contacting the resin and eluting the amine component contained in the anion exchange resin into crude 1,4BG is preferable.
- R 1 to R 3 each independently represents a hydrogen atom, an alkyl group, an alkenyl group, an aryl group, an alkoxy group, a hydroxy group, an amino group, an alkylthio group or an arylthio group.
- the group may further have a substituent, and the substituent may contain a hetero atom.
- R 1 to R 3 may be the same or different.
- a primary amide, a secondary amide, or a tertiary amide can be used as the carboxylic acid amide represented by the formula (2).
- N-alkenyl-substituted amides, N-aryl-substituted amides, and the like that is, carboxylic acid amides in which one or both of the substituents R a and R b are any of alkyl groups, alkenyl groups, and aryl groups are used.
- the substituents R a and R b may contain a hetero atom, and the substituents R a and R b may be the same or different.
- examples of the substituent R c on the carbonyl side include a hydrogen atom, an alkyl group, an alkenyl group, and an aryl group.
- the substituents R a to R c may be connected to each other to form a ring. From the viewpoint that side reactions and decomposition can be suppressed, the carbonyl-side substituent R c is preferably an alkyl group.
- the nitrogen atom equivalent concentration (hereinafter sometimes abbreviated as “nitrogen concentration”) is preferably 1 to 10,000 ppm by weight, particularly preferably 1 to 1000 ppm by weight.
- the temperature is usually 80 ° C. or higher, preferably 100 to 250 ° C., more preferably 120 to 200 ° C.
- the heating time varies depending on the heating temperature and is arbitrarily set, but is usually 1 minute to 100 hours, preferably 5 minutes to 10 hours.
- the method of this heat treatment is not particularly limited, but heating can be performed with a distillation tower, an extraction tank, piping, a heat exchanger, or the like.
- the crude 1,4BG to be subjected to the heat treatment preferably has a BGTF content of 0.04 to 0.5% by weight and a water concentration of 1.0 to 25% by weight. If the BGTF content in the crude 1,4BG to be subjected to the heat treatment is excessively high, the load in the treatment for reducing the BGTF concentration increases and the treatment cost is high. When the BGTF content is sufficiently low, the BGTF concentration reduction process by this heat treatment is unnecessary.
- the BGTF content of the crude 1,4BG to be subjected to the heat treatment is more preferably 0.05 to 0.45% by weight, still more preferably 0.06 to 0.4% by weight.
- the water concentration of crude 1,4BG to be subjected to the heat treatment is more preferably 2 to 20% by weight, and further preferably 5 to 16% by weight.
- the BGTF content or moisture concentration of the crude 1,4BG to be subjected to the heat treatment is out of the above preferred range, it is preferable to adjust components such as hydrogenation and distillation.
- crude 1,4BG with which it uses for heat processing is pH7 or more. That is, BGTF can be more efficiently reduced by heating crude 1,4BG containing a predetermined amount of amine and having a pH of 7 or more in a state containing moisture.
- crude 1,4BG having a pH of less than 7 due to heat treatment, THF is generated before being introduced into the reactor, causing an increase in the differential pressure of the distillation column or a loss of 1,4BG, for example.
- the crude 1,4BG has a pH of 7 or higher, the generation of THF during the heat treatment can be suppressed.
- the crude 1,4BG having a pH of 7 or more can be used as it is when the pH of the crude 1,4BG produced by the above-mentioned known technique is 7 or more. Even when the pH of the crude 1,4BG is less than 7, the pH can be set to 7 or more by the addition of the amine or contact with the anion exchange resin having an amine skeleton.
- the pH of crude 1,4BG to be subjected to the heat treatment should be 7 or more, and if it is too high, it will cause catalyst deterioration during the production of THF, so the pH should be 12 or less, for example 7.0 to 12.0. preferable.
- BGTF concentration reduction treatment by such heating, 0.01 to 0.35% by weight of BGTF as a raw material liquid described later is contained, and at least one of amine and amide is 1 to 2 in terms of nitrogen concentration. It is preferable to obtain a 1,4BG-containing liquid containing 1000 ppm by weight.
- 1,4BG may be concentrated by distillation purification or the like.
- the acid catalyst used in the present invention may be any acid catalyst as long as it has a pKa (acid dissociation constant) value of 4 or less and can cause 1,4BG to undergo a cyclodehydration reaction with THF.
- pKa acid dissociation constant
- sulfonic acid, cation exchange resin, heteropolyacid, phosphoric acid, and the like are preferable, organic acid or phosphoric acid not containing metal is more preferable, and organic sulfonic acid is particularly preferable.
- aromatic sulfonic acid derivatives such as p-toluenesulfonic acid, benzenesulfonic acid, orthotoluenesulfonic acid, and metatoluenesulfonic acid, chain forms such as butanesulfonic acid, hexanesulfonic acid, octanesulfonic acid, and nonanesulfonic acid
- aromatic sulfonic acid derivatives, and the like may have a functional group other than sulfonic acid in the carbon skeleton.
- These acid catalysts may be used alone or in combination of two or more.
- paratoluenesulfonic acid is particularly preferably used.
- organic sulfonic acids and the like are usually soluble in 1,4BG.
- the amount of the acid catalyst used is usually 0.01 to 20% by weight, preferably 0.05 to 10% by weight, particularly preferably 0.2 to 5% by weight as the concentration in the reaction solution in the reactor. .
- the acid catalyst can be added all at once at the start of the reaction or before the start of the reaction. However, in order to compensate for the deterioration of the catalyst with the passage of time, it is possible to continue the reaction more stably. It is preferable because it is effective.
- the amount of the acid catalyst added is 0.0001 to 0 as the concentration of the acid catalyst with respect to the amount of 1,4BG contained in the raw material over time, with respect to the amount of the raw material solution containing 1,4BG contained in the reactor over time. .1% by weight is preferable, and a concentration range of 0.0005 to 0.005% by weight is particularly preferable. Therefore, for example, a raw material liquid to which an acid catalyst is added so as to be in such a concentration range may be introduced into the reactor.
- the BGTF content of the 1,4BG-containing raw material liquid to be subjected to the reaction is 0.01 to 0.35 wt%, and at least one of amine and amide is contained at a nitrogen concentration of 1 to 1000 ppm by weight.
- a raw material liquid refers to components other than an acid catalyst among the components provided to the reactor of a dehydration cyclization reaction.
- the BGTF content of the raw material liquid is preferably 0.01 to 0.33% by weight, more preferably 0.02 to 0.30% by weight, and particularly preferably 0.03 to 0.16% by weight.
- the effect of the present invention that reduces the production of by-product solids by reducing BGTF derived from 1,4BG during the dehydration cyclization reaction is sufficient. Can't get to.
- the above effect increases as the amount of at least one of amine and amide increases.
- the amount of at least one of amine and amide is excessively large, the addition cost of at least one of amine and amide increases.
- At least one of the amine and the amide causes a decrease in THF productivity. Therefore, at least one of the amine and amide in the raw material liquid has a nitrogen concentration of 1 to 1000 ppm by weight, preferably 2 to 200 ppm by weight, more preferably 20 to 80 ppm by weight.
- the amount of amine in the raw material liquid is 1 to 1000 ppm by weight, preferably 2 to 200 ppm by weight, more preferably 20 ppm as the nitrogen concentration. ⁇ 80 ppm by weight.
- the amount of amide in the raw material liquid is 1 to 1000 ppm by weight, preferably 2 to 200 ppm by weight, more preferably 5 ppm as the nitrogen concentration. ⁇ 60 ppm by weight.
- the total amount of amine and amide in the raw material liquid is 1 to 1000 ppm by weight, preferably 2 to 200 ppm by weight, more preferably 20 to 80 ppm as the nitrogen concentration. Ppm by weight.
- concentration range of at least one of amine and amide when the lower limit is increased, the effect of the present invention is more manifested, and when the upper limit is decreased, the subsequent process tends to be reduced.
- a method of adding at least one of amine and amide to the raw material liquid, or contacting the raw material liquid with an anion exchange resin having an amine skeleton A method of eluting the amine component contained in the anion exchange resin into the raw material liquid is preferable.
- the amount eluted from the anion exchange resin is a polyamine, which is a general term for straight-chain aliphatic hydrocarbons in which two or more primary amino groups are bonded.
- polyamine is represented by the formula (1).
- a separation operation such as distillation may be performed on the raw material liquid after addition of at least one of amine and amide or contact with an anion exchange resin having an amine skeleton.
- the amine used here includes primary amines such as octylamine, nonylamine, 1-aminodecane, aniline and phenethylamine, secondary amines such as dipentylamine, dihexylamine, diheptylamine, dicyclohexylamine and N-methylaniline, and tributylamine.
- Tertiary amines such as tripentylamine, N, N-dimethylaniline, diamines such as 1,3-propanediamine, N, N-dimethyl-1,6-hexanediamine, N-butylpyrrole, N-butyl-2 , 3-dihydropyrrole, N-butylpyrrolidine, 2,3-dihydro-1H-indole and other 5-membered ring amines, 4-aminomethylpiperidine, 4-dimethylaminopyridine, 1,2,3,4-tetrahydroquinoline, 4-amino-5,6-dihydro-2-methylpyrimidine, , 3,5,6-tetramethylpyrazine, 3,6-dimethylpyridazine, etc., and 4-aminobutanol from the viewpoint of having a boiling point close to 1,4BG.
- Cyclic amino alcohols such as 2-aminobutanol, cyclic amines such as 2-ethylmorpholine, N-methoxycarbonylmorpholine, prolinol, 3-hydroxypiperidine, 4-hydroxypiperidine, tetrahydrofurfurylamine, and 3-aminotetrahydropyran.
- cyclic amines such as 2-ethylmorpholine, N-methoxycarbonylmorpholine, prolinol, 3-hydroxypiperidine, 4-hydroxypiperidine, tetrahydrofurfurylamine, and 3-aminotetrahydropyran.
- an elution fraction of an anion exchange resin containing a primary or secondary amine having at least one NH bond or a primary polyamine having an NH bond is preferable.
- Is a primary amine such as octylamine, nonylamine, 1-aminodecane, aniline, phenethylamine, dipentylamine, dihexylamine, diheptylamine, dicyclohexylamine, N-methylaniline and the like in terms of promoting the decomposition of BGTF.
- chain amino alcohols such as 4-aminobutanol and 2-aminobutanol, 2-ethylmorpholine, prolinol, 3-hydroxypiperidine, 4-hydroxypiperidine, tetrahydrofurfurylamine, 3-aminotetrahydro Cyclic amines such as pyran are preferred.
- 1-aminodecane, dihexylamine, prolinol, 3-hydroxypiperidine, 4-hydroxypiperidine, 4-amino are preferred because a compound having a boiling point of 160 to 260 ° C. under atmospheric pressure is preferably used. Examples include butanol and tetrahydrofurfurylamine.
- preferred amides for use in the present invention are those whose boiling point under atmospheric pressure is not lower than 1,4BG, and in terms of the stability of the compound, for example, acetamide, N-methylacetamide, N-ethylacetamide, Chain skeleton amides such as N, N-dimethylacetamide, aromatic amides such as benzamide, 2-pyrrolidone, N-methylpyrrolidone, N-ethylpyrrolidone, N-vinylpyrrolidone, 2-piperidone, N-methylpiperidone, etc.
- acetamide, N-methylacetamide, 2-pyrrolidone and N-methylpyrrolidone are mentioned in terms of the boiling point close to 1,4BG which is a raw material.
- 2-pyrrolidone and N-methylpyrrolidone are particularly preferred because they have a boiling point close to 1,4BG as a raw material and high stability.
- the raw material liquid used in the present invention may contain only one of the above amines, or may contain two or more.
- the raw material liquid used in the present invention may contain only one of the above amides, or may contain two or more.
- the raw material liquid used in the present invention may contain one or more of the above amines and one or more of the amides.
- amine and amide When at least one of amine and amide is added to the raw material liquid, it may be added to the raw material liquid before being introduced into the reactor, may be added to the raw material liquid in the reactor, or both. May be.
- the moisture concentration in the raw material liquid is not particularly limited. That is, the effect of reducing BGTF in the presence of at least one of an amine and an amide is achieved by the presence of water, but in the present invention, water is produced by the dehydration cyclization reaction of 1,4BG.
- the raw material liquid at the start of the dehydration cyclization reaction may or may not contain water. However, if an excessively large amount of water is contained in the raw material liquid, the reactor capacity becomes excessive with respect to the THF production capacity, and the dehydration cyclization reaction is also inhibited, so the water concentration is 25% by weight. The following is preferable.
- 1,4BG produced by various known production methods includes BGTF, 1-acetoxy-4-hydroxybutane, dehydrated dimer of 1,4-butanediol, and 3 dehydrated amount.
- by-products such as ⁇ -butyrolactone.
- the content of these by-products other than BGTF is not particularly limited, but it is preferable that the by-products other than BGTF are also small, and the content of these BGTF and by-products other than water in the raw material liquid is 0. It is preferably 3% by weight or less, particularly 0.05% by weight or less.
- the content of BGTF and the content of at least one of amine and amide in the raw material liquid to be subjected to the reaction may be in the above range, and as described above, the amine is added to the raw material liquid before being introduced into the reactor. And at least one of amide and amide may be added to the raw material liquid in the reactor, or both of them may be added.
- the BGTF content is reduced in advance by the above heat treatment or the like.
- the BGTF content is 0.01 to 0.35% by weight, preferably 0.01 to 0.33% by weight, more preferably 0.02 to 0.30% by weight, and particularly preferably 0.03 to 0.16%. It is preferable to introduce a weight percent raw material liquid into the reactor.
- the heat treatment liquid When heat treatment is performed in the presence of water and at least one of the above-mentioned amine and amide, the heat treatment liquid contains at least one of amine and amide.
- the heat treatment liquid By setting the amount of at least one of the amine and amide present during the treatment to an appropriate amount for the raw material liquid to be subjected to the reaction, the heat treatment liquid is directly introduced into the reactor as the raw material liquid to start the dehydration cyclization reaction. can do.
- at least one of amine and amide in the heat treatment liquid is insufficient, at least one of amine and amide may be added separately.
- the reactor for carrying out the cyclization dehydration reaction is not particularly limited, a fixed bed reactor filled with a solid catalyst such as a cation exchange resin, a suspension bed reactor using a solid catalyst, or A tank-type or tube-type reactor using a homogeneous acid catalyst that can be dissolved in the raw material can be used. It is also possible to obtain THF by discharging a solution containing THF and by-product water in the liquid phase part of the reactor from the reactor and purifying it in a subsequent step such as a distillation column. It is also possible to extract a part or the whole amount from the gas as a gas containing the generated THF and by-product water.
- the gas extracted from the reactor is condensed by the heat exchanger to obtain a condensate.
- This heat exchanger is a device that condensates and distills the distillate generated from the reactor, and the condensation is performed by exchanging heat between an external fluid that is a cooling liquid and a gas.
- the THF and by-product water produced by the distillation column are separated from the unreacted raw material, and the high-boiling components such as the unreacted raw material and the dimer are circulated to the reactor, or the THF and the by-product water produced through the gas phase. Is discharged as a gas from the gas phase portion in the reactor, whereby high boiling point by-products can be accumulated in the liquid phase portion in the reactor.
- dibutylene glycol which is a dehydrated dimer of 1,4BG
- THF trifluorohydrofuran
- some or all of these high-boiling byproducts accumulate in the liquid phase of the reactor.
- THF and by-product water discharged as gas may be cooled and condensed, and a part thereof may be circulated as reflux in the reactor.
- the reaction temperature which is the internal temperature of the liquid phase part in the reactor, is preferably 80 to 250 ° C., more preferably 100 to 200 ° C., and particularly preferably 120 to 180 ° C. At temperatures lower than this, the productivity of THF is significantly reduced, and at temperatures higher than this, it is necessary to increase the amount of by-products or to use an expensive material as a reactor material in order to use an acid catalyst. Absent.
- the reaction pressure may be any pressure, but is 10 to 1000 kPa as an absolute pressure, particularly preferably 100 to 500 kPa.
- the solution in the reactor contains, in addition to the raw material 1,4BG and the acid catalyst, THF produced by the dehydration cyclization reaction and water produced as a by-product. It may contain a high-boiling compound derived from impurities in 1,4BG, by-products generated from THF and 1,4BG, acetate ester of 1,4BG, and the like.
- the gas containing THF and by-product water generated is discharged from the gas phase part and condensed by a heat exchanger to obtain a condensate, part of which is returned to the gas phase part in the reactor as reflux.
- the composition of the condensed liquid can contain THF and by-product water in any concentration, but preferably the THF concentration is 30 to 95% by weight, particularly preferably 50 to 85% by weight. .
- this reaction produces
- a part of this condensate can be returned to the gas phase in the reactor as reflux, and the reflux ratio is preferably 0.001 or more and 30 or less, more preferably in the range of 0.01 to 10 Particularly preferably, it is in the range of 0.1 to 5. If the reflux ratio is too high, the required evaporation amount increases, which increases the cost of the heat source for heating and deteriorates the economy. If the reflux ratio is too low, the solids precipitation is reduced. The effect cannot be obtained, and mixing into the distillate condensate due to deterioration of separation of high-boiling components proceeds.
- the temperature at the time of introduction of the product gas containing THF and by-product water introduced into the heat exchanger is preferably 10 to 200 ° C., particularly preferably 60 to 100 ° C.
- the fluid can be discharged out of the process system continuously or intermittently from within a series of THF production processes (including not only the reactor but also the purification system at the latter stage of the reactor).
- the supply of the raw materials 1 and 4BG may be stopped once and the THF production may be stopped and discharged.
- the discharged liquid can be processed and disposed of by incineration.
- emitted liquid contains solid acid elution components, such as an acid catalyst or a cation exchange resin, it can also carry out industrial waste processing, such as incineration, after neutralizing.
- the 1,4BG concentration in the reaction solution in the reactor is preferable to ensure a sufficient 1,4BG concentration in the reaction solution in the reactor during the dehydration cyclization reaction. Specifically, it is preferable to control to 30 to 99% by weight, preferably 40 to 90% by weight, and more preferably 50 to 80% by weight.
- the 1,4BG concentration of the reaction solution is not more than the above upper limit, a rapid increase in the composition of the polymer, which is a high-boiling component, can be suppressed and reduced. If the polymer is excessively accumulated in the reactor, solid matter precipitation proceeds in the process, and the operation is hindered by clogging with dirt.
- the 1,4BG concentration in the reaction solution is too low, it indicates that the high-boiling components such as unreacted raw materials or dimers are not recovered, and the raw material consumption is increased.
- the amount of at least one of amine and amide in the reaction liquid in the reactor during the dehydration cyclization reaction is preferably 1 to 10,000 ppm by weight in terms of nitrogen concentration.
- the water concentration is preferably 0.1 to 10% by weight.
- the amount of at least one of amine and amide in the reaction liquid in the reactor during the dehydration cyclization reaction is less than 1 ppm by weight in nitrogen concentration, the effect of reducing BGTF and the effect of preventing the formation of by-product solids are sufficiently obtained If it exceeds 10000 ppm by weight, the productivity of THF is inhibited.
- the water concentration of the reaction liquid in the reactor during the dehydration cyclization reaction is less than 0.1% by weight, the effect of reducing BGTF and the effect of preventing the formation of by-product solids cannot be sufficiently obtained. If it exceeds 10% by weight, the dehydration cyclization reaction is inhibited.
- a more preferable water concentration is 1 to 6% by weight.
- the amount of at least one of amine and amide in the reaction liquid in the reactor during the dehydration cyclization reaction is 1 to 10,000 ppm by weight, preferably 1 to 4000 ppm by weight, more preferably 11 to 650 in terms of nitrogen concentration.
- the weight concentration is ppm
- the water concentration is preferably 0.1 to 10% by weight, more preferably 0.1 to 5% by weight, and still more preferably 0.1 to 3% by weight.
- the amount of amine in the reaction solution is 1 to 10,000 ppm by weight, preferably 8 to 800% by weight as the nitrogen concentration. ppm, more preferably 11 to 650 ppm by weight.
- the amount of amide in the reaction liquid is 1 to 10000 ppm by weight, preferably 8 to 800% by weight as the nitrogen concentration. ppm, more preferably 20 to 650 ppm by weight.
- the total amount of amine and amide in the reaction liquid is 1 to 10,000 ppm by weight as nitrogen concentration, preferably 8 to 800 weights. ppm, more preferably 11 to 650 ppm by weight.
- the content of at least one of the amine and amide in the raw material liquid at the start of the dehydration cyclization reaction is 1-1000 ppm by weight, and the amount of at least one of the amine and amide in the reaction liquid during the dehydration cyclization reaction If the amount of at least one of amine and amide increases due to prolonged operation or increase in the concentration of at least one of amine and amide in the raw material liquid, the reaction liquid is discharged. By doing so, it is preferable to suppress the amount of at least one of the amine and the amide in the reaction solution during the dehydration cyclization reaction to the upper limit or less. In addition, when the water concentration is outside the above preferred range, it is preferable to adjust the concentration by adding water or distilling water.
- the time when the dehydration cyclization reaction starts refers to the time when the raw material liquid is introduced into the reactor and the heating starts
- the time during the dehydration cyclization reaction refers to the time in the reactor after the start of the heating.
- the period during which the reaction liquid temperature is maintained at the predetermined reaction temperature.
- the reaction liquid in the reactor during the dehydration cyclization reaction is at least one of raw materials 1,4BG, acid catalyst, THF, water, high-boiling compounds derived from impurities in raw materials 1,4BG, BGTF, amines and amides.
- a mixed solution of by-products generated from THF and 1,4BG are examples of by-products generated from THF and 1,4BG.
- Example 1 A 1000 mL glass flask was charged with 350 g of crude 1,4BG and 35 g of anion exchange resin and stirred at room temperature for 2 hours, and then the anion exchange resin was filtered off. As a result of measuring the BGTF concentration in the liquid after adding 70 g of water to 320 g of the obtained filtrate, it was 0.2206% by weight. At this time, the water concentration in this liquid was 24.7 wt%, the 1,4BG concentration was 74.99 wt%, the content of polyamine eluted from the anion exchange resin was 110 ppm by weight in terms of nitrogen atom, The pH was 8.6.
- the amount of the distillate containing THF was 340.2 g.
- the composition of the distillate was 58.1% by weight of THF and 41.2% by weight of water.
- the yield of THF was 88.9%, and the production rate of THF was 51.1 g / hr.
- the residual liquid in the flask reactor was 25.4 g, the water concentration was 1.3 wt%, and the nitrogen concentration was 1603 wt ppm.
- the amount of solids in the residual liquid in the flask reactor was 0.6 mg.
- the yield of by-product solids (weight ppm) / THF yield was 2. The results are summarized in Table 1.
- Example 2 A 1000 mL glass flask was charged with 600 g of crude 1,4BG and 60 g of an anion exchange resin and stirred at room temperature for 2 hours, and then the anion exchange resin was filtered off. As a result of measuring the BGTF concentration in the liquid after adding 105 g of water to 520 g of the obtained filtrate, it was 0.2206% by weight. At this time, the water concentration in this liquid was 21.0 wt%, the 1,4BG concentration was 78.71 wt%, the polyamine content eluted from the anion exchange resin was 110 ppm by weight in terms of nitrogen atom, The pH was 8.6.
- Example 3 A 1000 mL glass flask was charged with 600 g of crude 1,4BG and 60 g of an anion exchange resin and stirred at room temperature for 2 hours, and then the anion exchange resin was filtered off. 4.0 g of the obtained filtrate was diluted with 400 g of crude 1,4BG, and a raw material 1,4BG containing a polyamine eluted from the anion exchange resin at a concentration of 1.1 wt ppm in terms of nitrogen atom (water concentration 0.029 wt%, 1,4BG concentration 99.7 wt%, nitrogen concentration 1.1 wtppm, BGTF concentration 0.2902 wt%). In addition, it was 7.0 as a result of measuring pH.
- Example 4 As the raw material 1,4BG, except that BGTF concentration was 0.3236 wt% and 4-hydroxypiperidine (abbreviated as “4OHP”) containing 46.0 ppm by weight in terms of nitrogen atom was used. Same as Example 3. The nitrogen concentration in the raw material liquid in the reactor at the start of the dehydration cyclization reaction was 56.0 ppm by weight. Also in the following examples and comparative examples, the nitrogen concentration in the raw material liquid in the reactor at the start of the dehydration cyclization reaction is substantially equal to the nitrogen atom equivalent concentration of the raw materials 1 and 4BG. 265.1 g of the distillate containing THF was extracted into a glass storage tank to obtain 27.5 g of a residual liquid in the flask reactor. The amount of solid matter in the residual liquid in the flask reactor was 0.3 mg. The yield of by-product solids (weight ppm) / THF yield was 1. The reaction results at this time are summarized in Table 1.
- Example 5 The reaction was performed in the same manner as in Example 3 except that 1,4BG containing 10.0 wt ppm of 4-hydroxypiperidine (4OHP) in terms of nitrogen atom was used as the raw material 1,4BG. 263.0 g of the distillate containing THF was extracted into a glass storage tank to obtain 36.9 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 0.8 mg. The yield of by-product solids (weight ppm) / THF yield was 3. The reaction results at this time are summarized in Table 1.
- Example 6 The reaction was carried out in the same manner as in Example 3 except that 1,4BG containing 1.1 wt ppm of 4-hydroxypiperidine (4OHP) in terms of nitrogen atom was used as the raw material 1,4BG. 260.9 g of a distillate containing THF was extracted into a glass storage tank to obtain 39.2 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 0.6 mg. The yield of by-product solids (weight ppm) / THF yield was 2. The reaction results at this time are summarized in Table 1.
- Example 7 The reaction was carried out in the same manner as in Example 3 except that 1,4BG containing 10.0 ppm by weight of 1-aminodecane in terms of nitrogen atom was used instead of 4-hydroxypiperidine as the raw material 1,4BG. 274.6 g of a distillate containing THF was extracted into a glass storage tank to obtain 25.3 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 1.2 mg. The yield of by-product solids (weight ppm) / THF yield was 4. The reaction results at this time are summarized in Table 1.
- Example 8 The reaction was carried out in the same manner as in Example 3 except that instead of 4-hydroxypiperidine, 1,4BG containing 10.0 wt ppm of tri-n-butylamine in terms of nitrogen atom was used as the raw material 1,4BG. 264.9 g of the distillate containing THF was extracted into a glass storage tank to obtain 35.1 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 0.8 mg. The yield of by-product solids (weight ppm) / THF yield was 3. The reaction results at this time are summarized in Table 1.
- Example 9 Example 3 except that 1,4BG containing 2-pyrrolidone (abbreviated as “2P”) instead of 4-hydroxypiperidine and containing 10.0 ppm by weight in terms of nitrogen atom was used as the raw material 1,4BG.
- the reaction was performed in the same manner. 265.8 g of distillate containing THF was extracted into a glass storage tank to obtain 34.2 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 0.9 mg. The yield of by-product solids (weight ppm) / THF yield was 3.
- Table 1 The reaction results at this time are summarized in Table 1.
- Example 1 The reaction was performed in the same manner as in Example 3 except that 1,4BG having a BGTF concentration of 0.3236% by weight and a nitrogen concentration of 0.1 ppm by weight or less was used as the raw material 1,4BG. 260.9 g of a distillate containing THF was extracted into a glass storage tank to obtain 34.7 g of a residual liquid in the flask reactor. The amount of solids in the residual liquid in the flask reactor was 140 mg. The yield of by-product solids (weight ppm) / THF was 54. The reaction results at this time are summarized in Table 2.
- Example 6 The reaction was carried out in the same manner as in Example 3 except that 1,4BG containing 2-pyrrolidone in a nitrogen atom equivalent concentration of 2000 ppm by weight was used as the raw material 1,4BG.
- the distillation rate of THF was 12 g / h (1/4 or less of the example), and the THF conversion reaction was significantly suppressed.
- the reaction results at this time are summarized in Table 2.
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Abstract
Description
具体的に、特許文献3には、ポリマーなどの副生固形物の析出が、運転を困難にすることが記載されており、1,4BG合成時の反応副生物であって、原料1,4BG中に不純物として含まれる2-(4-ヒドロキシブトキシ)-テトラヒドロフラン(以下、「BGTF」と略記することがある。)由来の固形物の生成について記載されている。このようなTHF製造時の副生固形物の析出を回避するべく、特許文献3には、触媒の前処理法の規定、あるいは窒素含有量を低く保持することなどが記載されている。
[2] 反応器内で、pKa値が4以下の酸触媒の存在下に、1,4-ブタンジオールの脱水環化反応を行うことによりテトラヒドロフランを製造する方法であって、反応器内の反応液が、アミン及びアミドのうち少なくとも一方を窒素原子換算濃度で1重量ppm以上、10000重量ppm以下含む、テトラヒドロフランの製造方法。
[3] 前記反応器内の反応液が、アミン及びアミドのうち少なくとも一方を窒素原子換算濃度で1重量ppm以上、10000重量ppm以下含む、[1]に記載のテトラヒドロフランの製造方法。
[4] 前記反応器内の反応液が、水分を0.1重量%以上、10重量%以下含む、[1]ないし[3]のいずれか1に記載のテトラヒドロフランの製造方法。
[5] 前記反応器内の気相部に存在するテトラヒドロフラン及び水を含むガスを反応器外へ抜き出す工程を有する、[1]ないし[4]のいずれか1に記載のテトラヒドロフランの製造方法。
[6] 前記反応器内の反応液の温度が80℃以上、250℃以下の範囲である、[1]ないし[5]のいずれか1に記載のテトラヒドロフランの製造方法。
[7] 粗1,4-ブタンジオールを、アミン及びアミドのうち少なくとも一方の存在下で80℃以上に加熱することにより、2-(4-ヒドロキシブトキシ)-テトラヒドロフラン含有量を低減した後、前記反応器に供給する工程を有する、[1]ないし[6]のいずれか1に記載のテトラヒドロフランの製造方法。
本発明で使用する1,4BGは公知の方法により得ることができる。
例えば、ブタジエンのジアセトキシ化により得た1,4-ジアセトキシ-2-ブテンを水素化した後、加水分解することにより1,4BGを製造することができる。或いは無水マレイン酸の水素化により得た1,4BG、レッペ法によりアセチレンから誘導した1,4BG、プロピレンの酸化を経由して得られる1,4BG、発酵法により得た1,4BGなどを使用することもできる。
このため、本発明では、必要に応じて、前述のような公知の方法で製造された粗1,4BG中のBGTF濃度を低減するための処理を施した後、反応器に供給することが好ましい。
また、上記置換基Ra~Rcはそれぞれ互いに連結して環を形成していてもよい。副反応や分解等を抑制できるという観点から、カルボニル側の置換基Rcとしてはアルキル基が好ましい。
加熱処理に供する粗1,4BG中のBGTF含有量が過度に高いとBGTF濃度低減のための処理における負荷が増大して処理コストが高くつく。BGTF含有量が十分に低い場合には、この加熱処理によるBGTF濃度の低減処理は不要となる。加熱処理に供する粗1,4BGのBGTF含有量は、より好ましくは0.05~0.45重量%であり、更に好ましくは0.06~0.4重量%である。
pH7未満の粗1,4BGでは、加熱処理により、反応器に導入する前にTHFが生成してしまい、例えば蒸留塔の差圧上昇を引き起こしたり、1,4BGのロスとなったりする。一方、pH7以上の粗1,4BGであれば加熱処理時のTHFの生成を抑制することができる。pH7以上の粗1,4BGには、上記公知技術により製造された粗1,4BGのpHが7以上である場合にはそのまま用いることができる。また、この粗1,4BGのpHが7未満の場合でも、上述のアミン添加あるいはアミン骨格を有する陰イオン交換樹脂との接触などによりpHを7以上とすることができる。
本発明で用いる酸触媒は、pKa(酸解離定数)の値が4以下で且つ1,4BGをTHFに脱水環化反応させることができるものであればよく、任意の酸触媒を用いることができるが、好ましくは、スルホン酸、陽イオン交換樹脂、ヘテロポリ酸、リン酸などであり、更に好ましくは金属を含有しない有機酸あるいはリン酸であり、特に好ましくは有機スルホン酸である。具体的には、パラトルエンスルホン酸、ベンゼンスルホン酸、オルトトルエンスルホン酸、メタトルエンスルホン酸などの芳香族スルホン酸誘導体、ブタンスルホン酸、ヘキサンスルホン酸、オクタンスルホン酸、ノナンスルホン酸などの鎖状の脂肪族スルホン酸誘導体などが挙げられ、これらは炭素骨格内にスルホン酸以外の官能基を有していても差し支えない。これらの酸触媒は1種を単独で用いてもよく、2種以上を混合して用いてもよい。酸触媒としては、特に好ましくはパラトルエンスルホン酸が用いられる。
なお、酸触媒のうち、有機スルホン酸などは、通常、1,4BGに溶解可能である。
本発明においては、反応に供する1,4BG含有原料液のBGTF含有量を0.01~0.35重量%とし、アミン及びアミドのうち少なくとも一方を窒素濃度で1~1000重量ppm含有させることを特徴とする。なお、本発明において、原料液とは、脱水環化反応の反応器に供する成分のうち、酸触媒以外の成分をさす。
従って、原料液中のアミン及びアミドのうち少なくとも一方は、窒素濃度として1~1000重量ppm、好ましくは2~200重量ppm、より好ましくは20~80重量ppmとする。
また、本発明に係る原料液中にアミドのみを含み、アミンを含まない場合、原料液中のアミド量は、窒素濃度として1~1000重量ppm、好ましくは2~200重量ppm、より好ましくは5~60重量ppmである。
また、原料液中にアミンとアミドのいずれも含む場合、原料液中のアミンとアミドの合計量は、窒素濃度として1~1000重量ppm、好ましくは2~200重量ppm、より好ましくは20~80重量ppmである。
アミン及びアミドのうち少なくとも一方の濃度範囲は、下限が上がると本発明の効果をより発現し、上限が下がると後工程の処理が軽減される傾向にある。
アミン及びアミドのうち少なくとも一方を添加した後あるいはアミン骨格を有する陰イオン交換樹脂などに接触させた後の原料液に蒸留などの分離操作を行ってもよい。
また、本発明で用いる原料液には、上記のアミンの1種又は2種以上とアミドの1種又は2種以上が含まれていてもよい。
ただし、原料液中に過度に大量の水が含まれていると、THFの生産能力に対して、反応器容量が過大となり、更に脱水環化反応も阻害されるため、水分濃度は25重量%以下であることが好ましい。
これら、BGTF以外の副生物の含有量については、特に制限はないが、これらBGTF以外の副生物についても、少ないことが好ましく、原料液中のこれらBGTF及び水以外の副生物の含有量は0.3重量%以下、特に0.05重量%以下であることが好ましい。
ただし、加熱処理液中のアミン及びアミドのうち少なくとも一方が不足する場合には、別途アミン及びアミドのうち少なくとも一方を添加してもよい。
本発明において、環化脱水反応を行う反応器は、特に限定されるものではなく、陽イオン交換樹脂などの固体触媒を充填した固定床反応器、固体触媒を用いた懸濁床反応器又は、原料に溶解可能な均一系酸触媒を用いた槽型或いは管型の反応器を使用することができる。また、反応器内の液相部のTHF及び副生水を含む溶液を反応器から排出して蒸留塔などの後工程で精製してTHFを得ることも可能であるが、反応器の気相から一部、あるいは全量を、生成したTHF及び副生水を含むガスとして抜き出すことも可能である。この場合、反応器から抜き出されたガスは熱交換器により凝縮されて凝縮液を得る。この熱交換器は、反応器から生じる留出物を凝縮液化させる装置であり、該凝縮液化は、冷却液である外部流体とガスとを熱交換させることにより行われる。
同様に、脱水環化反応中の反応器内の反応液の水分濃度が0.1重量%よりも少ないとBGTFの低減効果、副生固形物の生成防止効果を十分に得ることができず、10重量%よりも多いと脱水環化反応が阻害される。より好ましい水分濃度は1重量%~6重量%である。
なお、脱水環化反応中の反応器内の反応液中にアミンのみを含み、アミドを含まない場合、反応液中のアミン量は、窒素濃度として1~10000重量ppm、好ましくは8~800重量ppm、より好ましくは11~650重量ppmである。
また、脱水環化反応中の反応器内の反応液中にアミドのみを含み、アミンを含まない場合、反応液中のアミド量は、窒素濃度として1~10000重量ppm、好ましくは8~800重量ppm、より好ましくは20~650重量ppmである。
また、脱水環化反応中の反応器内の反応液中にアミンとアミドを含む場合、反応液中のアミンとアミドの合計量は、窒素濃度として1~10000重量ppm、好ましくは8~800重量ppm、より好ましくは11~650重量ppmである。
また、水分濃度が上記好適範囲を外れる場合は水分の添加や水分の留出により濃度調整することが好ましい。
また、脱水環化反応中の反応器内の反応液とは原料1,4BGや酸触媒、THF、水、原料1,4BG中の不純物由来の高沸点化合物、BGTF、アミン及びアミドのうち少なくとも一方、ならびにTHFと1,4BGから生成される副生物等の混合溶液をさす。
1,4-ブタンジオール、テトラヒドロフラン及び2-(4-ヒドロキシブトキシ)-テトラヒドロフランの分析はガスクロマトグラフィーにより行い、クロマトグラムのピーク面積比率により算出した。即ち、100重量%から水分濃度(重量%)を差し引いた値を算出し、水分濃度を差し引いた後の重量%分に、ガスクロマトグラフィーの各成分の面積比率を乗じた。
窒素の分析は、試料をアルゴン・酸素雰囲気内で燃焼させ、発生した燃焼ガスを燃焼・減圧化学発光法を用いた微量窒素計(三菱化学アナリテック社製、TN-10型)で分析することにより行った。
1000mLのガラス製フラスコに粗1,4BGを350g、陰イオン交換樹脂を35g仕込み、室温で2時間攪拌した後、陰イオン交換樹脂を濾別した。得られた濾液320gに水を70g添加した後の液中のBGTF濃度を測定した結果、0.2206重量%であった。このとき、この液中の水分濃度は24.7重量%、1,4BG濃度は74.99重量%、陰イオン交換樹脂から溶出したポリアミンの含有量は窒素原子換算濃度で110重量ppmであり、pHは8.6であった。
1000mLのステンレス製オートクレーブに本溶液を充填し、オートクレーブ内を窒素ガスで置換した後、170℃で2時間加熱した。加熱処理液の分析を行った結果、BGTF濃度が0.1522重量%に低減していた。この加熱処理液(水分濃度24.7重量%、1,4BG濃度75.0重量%、窒素濃度110ppm、BGTF濃度0.1522重量%)を原料液としてTHFの製造を行った。
1000mLのガラス製フラスコに粗1,4BGを600g、陰イオン交換樹脂を60g仕込み、室温で2時間攪拌した後、陰イオン交換樹脂を濾別した。得られた濾液520gに水を105g添加した後の液中のBGTF濃度を測定した結果、0.2206重量%であった。このとき、この液中の水分濃度は21.0重量%、1,4BG濃度は78.71重量%、陰イオン交換樹脂から溶出したポリアミンの含有量は窒素原子換算濃度で110重量ppmであり、pHは8.6であった。
1000mLのステンレス製オートクレーブに本溶液を充填し、オートクレーブ内を窒素ガスで置換した後、170℃で2時間加熱した。加熱処理液の分析を行った結果、BGTF濃度が0.1544重量%に低減していた。
このときの反応結果を表1にまとめて示す。
1000mLのガラス製フラスコに粗1,4BGを600g、陰イオン交換樹脂を60g仕込み、室温で2時間攪拌した後、陰イオン交換樹脂を濾別した。得られた濾液4.0gを粗1,4BG400gで希釈し、陰イオン交換樹脂から溶出したポリアミンを窒素原子換算濃度で1.1重量ppm含有する原料1,4BG(水分濃度0.029重量%、1,4BG濃度99.7重量%、窒素濃度1.1重量ppm、BGTF濃度0.2902重量%)を調製した。なお、pHを測定した結果7.0であった。
留出のためのガラス製の冷却管を設置したガラス製の500mLフラスコ反応器に、該原料1,4BG300.0gを加え、パラトルエンスルホン酸1.50g(反応液に対して0.5重量%)を仕込み、オイルバスを使用して実施例1と同様にして145℃で反応蒸留を行ってTHFを含む留出液271.0gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液28.8gを得た。フラスコ反応器内の残液のうちの固形物量は0.9mgであった。副生固形物の収率(重量ppm)/THF収率は3であった。
なお、脱水環化反応開始時の反応器内の原料液中の窒素濃度は1.1重量ppmであった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、BGTF濃度が0.3236重量%で、4-ヒドロキシピペリジン(「4OHP」と略記する。)を窒素原子換算濃度で56.0重量ppm含む1,4BGを用いた以外は、実施例3と同様にした。なお、脱水環化反応開始時の反応器内の原料液中の窒素濃度は56.0重量ppmであった。以下の実施例及び比較例においても、脱水環化反応開始時の反応器内の原料液中の窒素濃度は、原料1,4BGの窒素原子換算濃度とほぼ等しい。
THFを含む留出液265.1gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液27.5gを得た。フラスコ反応器内の残液のうちの固形物量は0.3mgであった。副生固形物の収率(重量ppm)/THF収率は1であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジン(4OHP)を窒素原子換算濃度で10.0重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液263.0gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液36.9gを得た。フラスコ反応器内の残液のうちの固形物量は0.8mgであった。副生固形物の収率(重量ppm)/THF収率は3であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジン(4OHP)を窒素原子換算濃度で1.1重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液260.9gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液39.2gを得た。フラスコ反応器内の残液のうちの固形物量は0.6mgであった。副生固形物の収率(重量ppm)/THF収率は2であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジンの替わりに1-アミノデカンを窒素原子換算濃度で10.0重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液274.6gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液25.3gを得た。フラスコ反応器内の残液のうちの固形物量は1.2mgであった。副生固形物の収率(重量ppm)/THF収率は4であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジンの替わりにトリ-n-ブチルアミンを窒素原子換算濃度で10.0重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液264.9gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液35.1gを得た。フラスコ反応器内の残液のうちの固形物量は0.8mgであった。副生固形物の収率(重量ppm)/THF収率は3であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジンの替わりに2-ピロリドン(「2P」と略記する。)を窒素原子換算濃度で10.0重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液265.8gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液34.2gを得た。フラスコ反応器内の残液のうちの固形物量は0.9mgであった。副生固形物の収率(重量ppm)/THF収率は3であった。
このときの反応結果を表1にまとめて示す。
原料1,4BGとして、BGTF濃度0.3236重量%で、窒素濃度0.1重量ppm以下の1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液260.9gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液34.7gを得た。フラスコ反応器内の残液のうちの固形物量は140mgであった。副生固形物の収率(重量ppm)/THF収率は54であった。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、陰イオン交換樹脂から溶出したポリアミンを窒素原子換算濃度で0.5重量ppm含有する1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液272.1gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液27.9gを得た。フラスコ反応器内の残液のうちの固形物量は180mgであった。副生固形物の収率(重量ppm)/THF収率は62であった。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジン(4OHP)を窒素原子換算濃度で0.5重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液267.6gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液32.4gを得た。フラスコ反応器内の残液のうちの固形物量は110mgであった。副生固形物の収率(重量ppm)/THF収率は39であった。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、2N-NaOH水溶液をNa原子換算濃度で100.0重量ppm含むように添加した1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液274.0gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液26.0gを得た。フラスコ反応器内の残液のうちの固形物量は120mgであった。副生固形物の収率(重量ppm)/THF収率は43であった。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、25%-アンモニア水溶液を窒素原子換算濃度で10.0重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
THFを含む留出液268.4gをガラス製の貯槽に抜き出し、フラスコ反応器内に残液31.6gを得た。フラスコ反応器内の残液のうちの固形物量は210mgであった。副生固形物の収率(重量ppm)/THF収率は76であった。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、2-ピロリドンを窒素原子換算濃度で2000重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
本例では、THFの留出速度は12g/h(実施例の1/4以下)となり、THF化反応が顕著に抑制された。
このときの反応結果を表2にまとめて示す。
原料1,4BGとして、4-ヒドロキシピペリジンを窒素原子換算濃度で15000重量ppm含む1,4BGを用いた以外は、実施例3と同様に反応を行った。
本例では、内液温度が145℃に達しても、留出物は得られなかった。その後、内液温度を160℃まで加熱したが、内液温度が160℃に達しても、留出物は得られなかった。
このときの反応結果を表2にまとめて示す。
また、比較例6、7より、1,4BG含有原料液のアミン及びアミドのうち少なくとも一方の量が多いとTHFの生産性が低下し、過度に多いと反応が不可能となることが分かる。
Claims (7)
- 反応器内で、pKa値が4以下の酸触媒の存在下に、1,4-ブタンジオールの脱水環化反応を行うことによりテトラヒドロフランを製造する方法であって、反応に供する1,4-ブタンジオールを含む原料液が、2-(4-ヒドロキシブトキシ)-テトラヒドロフランを0.01~0.35重量%、アミン及びアミドのうち少なくとも一方を窒素原子換算濃度で1重量ppm以上、1000重量ppm以下含む、テトラヒドロフランの製造方法。
- 反応器内で、pKa値が4以下の酸触媒の存在下に、1,4-ブタンジオールの脱水環化反応を行うことによりテトラヒドロフランを製造する方法であって、反応器内の反応液が、アミン及びアミドのうち少なくとも一方を窒素原子換算濃度で1重量ppm以上、10000重量ppm以下含む、テトラヒドロフランの製造方法。
- 前記反応器内の反応液が、アミン及びアミドのうち少なくとも一方を窒素原子換算濃度で1重量ppm以上、10000重量ppm以下含む、請求項1に記載のテトラヒドロフランの製造方法。
- 前記反応器内の反応液が、水分を0.1重量%以上、10重量%以下含む、請求項1ないし3のいずれか1項に記載のテトラヒドロフランの製造方法。
- 前記反応器内の気相部に存在するテトラヒドロフラン及び水を含むガスを反応器外へ抜き出す工程を有する、請求項1ないし4のいずれか1項に記載のテトラヒドロフランの製造方法。
- 前記反応器内の反応液の温度が80℃以上、250℃以下の範囲である、請求項1ないし5のいずれか1項に記載のテトラヒドロフランの製造方法。
- 粗1,4-ブタンジオールを、アミン及びアミドのうち少なくとも一方の存在下で80℃以上に加熱することにより、2-(4-ヒドロキシブトキシ)-テトラヒドロフラン含有量を低減した後、前記反応器に供給する工程を有する請求項1ないし6のいずれか1項に記載のテトラヒドロフランの製造方法。
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