Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C67/00—Preparation of carboxylic acid esters
  • C07C67/24—Preparation of carboxylic acid esters by reacting carboxylic acids or derivatives thereof with a carbon-to-oxygen ether bond, e.g. acetal, tetrahydrofuran
  • C07C67/26—Preparation of carboxylic acid esters by reacting carboxylic acids or derivatives thereof with a carbon-to-oxygen ether bond, e.g. acetal, tetrahydrofuran with an oxirane ring

Definitions

• the present invention relates to a method for producing hydroxyalkyl (meth) atarylate by reacting (meth) acrylic acid and alkylene oxide in the presence of a catalyst.
• a catalyst In the method of producing hydroxyalkyl (meth) arylate by reacting (meth) acrylic acid and alkylene oxide, a catalyst is usually used, and examples of the above-mentioned catalyst include a chromium compound and the like. Homogeneous catalysts such as iron compounds are said to be suitable.
• the regulations for various types of drainage and exhaust gases etc. have become strict in terms of environment and health, and as with the case, there is a growing concern that the disposal of catalysts etc. is also concerned about their harmfulness. Therefore, it is desirable to reduce the amount of catalyst used in the manufacturing process.
• dialkylene glycol mono (meth) atarylates which is a di-adduct of alkylene oxide as a by-product which becomes an impurity.
• dialkyl glycol since (alkylene) oxide alone is dangerous, (meth) acrylic acid is charged in advance.
• JP-A 2004-10602 discloses alkylene. Methods and the like for suppressing the byproduct of a diadduct have been proposed by increasing the catalyst concentration relative to the amount of (meth) acrylic acid in the reaction liquid at the start of the reaction by charging the oxide.
• the suppression effect of the di-adduct by-product may also be required, so that the yield of the hydroxyalkyl (meth) atalylate, which is the target product, is further improved and the di-adduct It is required to suppress by-products. Therefore, it was necessary to propose a catalyst recycling technology that would simplify the process and would not complicate the process and a catalyst recycling technology that could reduce the cost of alkali treatment.
• the problem to be solved by the present invention is to provide a method for producing hydroxyalkyl (meth) atarylates which can realize low production cost.
• the present inventors diligently studied to solve the above problems.
• the amount of an acid component such as (meth) acrylic acid in the reaction solution always satisfies the specified molar ratio range with respect to the amount of catalyst.
• the catalyst itself can be effectively inhibited from being inactive by using a novel means of maintaining the reaction system in such a way that the catalyst activity can be sufficiently exerted just by using it as it is in the next reaction. It was possible to reduce the amount of catalyst used and the treatment cost, and to solve the problems described above. As a result, in a preferred embodiment, it has also become possible to dispense with the replenishment of a new catalyst and the reactivation of the catalyst after use.
• the ratio (molar ratio) of the amount of acid component to the amount of catalyst is always calculated within a specific range. It has been found that the catalyst inertness can be effectively suppressed and recycled efficiently if it is maintained as long as
• dialkylene mono- (meth) atalylate is supplied into the reaction system to allow the di-adduct to coexist in the reaction solution
• the novel means of supplying dialkylene glycol mono (meth) atalylate prior to the reaction is used in the reaction of (meth) acrylic acid with alkylene oxide. It has been found that the formation of by-products can be suppressed more effectively, the yield of the desired product, hydroxyalkyl (meth) atalilate can be improved, and the problems described above can be solved.
• the present inventors separately supply and coexist a byproduct diadduct, even if this is a non-equilibrium reaction (
• the supply of dialkylene glycol mono (meth) atalylate is made prior to the reaction to realize that the formation thereof can be effectively suppressed, and the hydroxyalkyl which is the desired product in a high yield It has been found that (meth) atarilate can be obtained.
• the present invention has been completed in this manner. Therefore, among the methods for producing hydroxyalkyl (meth) atarylates to be used in the present invention, the first method is to react (meth) atalic acid with alkylene oxide in the presence of a catalyst to produce hydroxyalkyl ( In the method of producing the (meth) atalylate, the amount of the acid component with respect to the amount of the catalyst in the reaction solution is calculated so as to maintain the molar ratio of not less than 0.010 and ) The reaction solution after distilling off atarilate is used for the next reaction.
• the second method is a method of producing hydroxyalkyl (meth) atalylate by reacting (meth) acrylic acid with alkylene oxide in the presence of a catalyst, and in the reaction system, It is characterized in that glycol mono (meth) atalylate is supplied so that dialkylene glycol mono (meth) atalylate coexists in the reaction solution. It is also a preferred embodiment to incorporate part of the first method into the second method. That is, if the amount of the acid component with respect to the amount of the catalyst in the reaction solution is calculated so as to maintain a molar ratio of not less than 0. 010, the reaction solution will contain (meth) acrylic acid.
• the reaction solution after distilling off the hydroxyalkyl (meth) atalylate in the first method is reused for the reaction of (meth) acrylic acid and alkoxide.
• the amount of the dialkylene glycol mono (meth) atalylate coexistent is calculated as the molar ratio of the amount of the catalyst in the reaction solution to 2: LOO
• the dialkylene glycol mono (meth) atalylate can be previously supplied before the reaction, and the dialkyl glycol di (di) contained in the reaction solution after distilling off the hydroxyalkyl (meth) atalylate.
• Alkylene glycol mono (meth) atalylate can be used to feed into the reaction system.
• the catalyst can be a homogeneous catalyst containing a chromium compound.
• the method for producing hydroxyalkyl (meth) atarylates (hereinafter sometimes referred to as the production method of the present invention) applicable to the present invention is, as described above, also for the first and second offset methods.
• (meth) acrylic acid is reacted with an alkylene oxide in the presence of a catalyst to produce a hydroxyalkyl (meth) arylate.
• Both the first and second methods apply to all known or previously proposed methods for producing hydroxyalkyl (meth) atarylates by reaction of (meth) acrylic acid with alkylene oxide. It is possible to
• (Meth) acrylic acid that can be used in the production method of the present invention means acrylic acid and Z or methacrylic acid.
• the alkylene oxide which can be used in the production method of the present invention is not limited.
• an alkylene oxide having 2 to 6 carbon atoms is preferable, and an alkylene oxide having 2 to 4 carbon atoms is more preferable.
• ethylene oxide, propylene oxide, butylene oxide and the like can be mentioned. Among them, ethylene oxide and propylene oxide are particularly preferable.
• the recycling method of using the catalyst of the present invention in the next reaction is particularly effective when the alkylene oxide used is ethylene oxide, because the effect of suppressing catalyst deactivation is high. It becomes a preferable form.
• the alkylene oxide used is ethylene oxide
• the effect of suppressing catalyst deactivation is high. It becomes a preferable form.
• propylene oxide although the effect of suppressing the catalyst inactivation is effective, there are aspects in which the catalyst is less likely to be inactive than in the case of ethylene oxide.
• propylene oxide by adapting the production method of the present invention, it is possible to increase the number of times of catalyst recycling, which is beneficial.
• butylene oxide can also be effective in suppressing catalyst inactivation.
• the amount relationship between the total supply amount of (meth) acrylic acid and the total supply amount of alkylene oxide in the reaction of (meth) acrylic acid and alkylene oxide is limited.
• the alkylene oxide content is 1 mole or more with respect to 1 mole of (meth) acrylic acid.
• S is preferred, more preferably 1. 0 to 10 monole, still more preferably 1. 0 to 5.0 monole, Particularly preferably, it is 1. 0 to 3.0 mol, and most preferably 1. 0 to 2.0 mol.
• the alkylene oxide content is less than 1.0 mol with respect to 1 mol of (meth) acrylic acid, the reaction may be difficult to progress, and the reaction conversion rate is lowered.
• Examples of the catalyst that can be used in the production method of the present invention include all homogeneous catalysts soluble in a reaction solution containing (meth) acrylic acid and alkylene oxide, and the limitation is not limited. Specifically, chromium (Cr) compounds, iron (Fe) compounds, yttrium (Y) compounds, lanthanum (La) compounds, cerium (Ce) compounds, tungsten (WM composites, zirconium!
• chromium (Cr) compounds which contain chromium (Cr) compounds and Z or iron (Fe) compounds and which are soluble in the reaction solution are more preferable.
• the homogeneous catalyst which is soluble in the reaction solution is further preferred, and the chromium (Cr) compound is also preferred, and the homogeneous catalyst which is soluble in the reaction solution is most preferred, particularly the catalyst in the first method described later.
• chromium (Cr) compound Containing chromium (Cr) compound as the reaction liquid
• the chromium (Cr) compound is preferred because a more remarkable effect is obtained. It is more preferable to use a homogeneous catalyst soluble in the reaction solution. Yes.
• the chromium (Cr) compound is not limited, and includes a compound having a chromium (Cr) atom in the molecule and being soluble in the reaction solution.
• Specific examples include chromium chloride, acetylacetonatochromium, chromium formate, chromium acetate, chromium octanoate, chromium iso-octoate, chromium acrylate, chromium methacrylate, sodium dichromate, chromium dibutyldithiocarbamate, and the like.
• the iron (Fe) compound is not limited and includes compounds having an iron (Fe) atom in the molecule and being soluble in the reaction solution. Specifically, iron powder, iron chloride, iron formate, iron acetate, iron acrylate, iron methacrylate and the like can be mentioned.
• the yttrium (Y) compound is not limited and includes compounds having an yttrium (Y) atom in the molecule and being soluble in the reaction liquid. Specific examples thereof include acetylacetonelithium, yttrium chloride, yttrium acetate, yttrium nitrate, yttrium sulfate, yttrium arylate and yttrium methacrylate.
• the lanthanum (La) compound is not limited, and includes a compound having a lanthanum (La) atom in the molecule and being soluble in the reaction solution. Specific examples thereof include acetylacetone lanthanum, lanthanum lanthanide, lanthanum acetate, lanthanum nitrate, lanthanum sulfate, lanthanum acrylate and lanthanum methacrylate.
• the cerium (Ce) compound is not limited and includes a compound having a cerium (Ce) atom in the molecule and being soluble in the reaction solution. Specific examples thereof include acetylacetone cerium, cerium chloride, cerium acetate, cerium nitrate, cerium sulfate, cerium acrylate, cerium methacrylate and cerium methacrylate.
• the tungsten (W) compound is not limited and includes a compound having a tungsten (W) atom in the molecule and being soluble in the reaction liquid. Specific examples include chlorinated tungsten, tungsten acrylate and tungsten methacrylate.
• the zirconium (Zr) compound is not limited and includes compounds having a zirconium (Zr) atom in the molecule and being soluble in the reaction solution. Specifically, acetylacetonate zirconium, zirconium chloride, zirconium acetate, zirconium nitrate, zirconium sulfate, zirconium acrylate, zirconium methacrylate, zirconium butoxide, zirconium propoxide, zirconium chloride, zirconium acetate, zirconium acetate And zircolate nitrate, zircolate acrylate and zirco methacrylate.
• the titanium (Ti) compound is not limited and includes a compound having a titanium (Ti) atom in the molecule and being soluble in the reaction solution. Specific examples thereof include titanium chloride, titanium nitrate, titanium sulfate, titanium methoxide, titanium ethoxide, titanium propoxide, titanium isopropoxide, titanium acrylate and titanium methacrylate.
• Vanadium The compound of VM is not limited and includes compounds having a vanadium (V) atom in the molecule and being soluble in the reaction solution. Examples include acetone vanadium, vanadium chloride, vanadium naphthenate, vanadium acrylate and vanadium methacrylate and the like.
• the phosphorus (P) compound is not limited, and includes a compound having a phosphorus (P) atom in the molecule and being soluble in the reaction solution.
• alkyl phosphines such as trimethyl phosphine, tributyl phosphine, trioctyl phosphine, triphenyl phosphine, tritolyl phosphine and 1, 2-bis (diphenyl phosphine) ethane and the (meth) acrylic acid thereof
• Examples include quaternary phosphonium salts such as salts.
• the aluminum (A1) compound is not particularly limited, and includes a compound having an aluminum (A1) atom in the molecule and being soluble in the reaction solution. Specifically, Seton aluminum, chloride aluminum, aluminum acetate, aluminum nitrate, aluminum sulfate, aluminum ethoxide, aluminum isopropoxide, aluminum acrylate, aluminum methacrylate and the like can be mentioned.
• the molybdenum (Mo) compound is not limited and includes a compound having a molybdenum (Mo) atom in the molecule and being soluble in the reaction solution. Specific examples include molybdenum chloride, molybdenum acetate, molybdenum acrylate and molybdenum methacrylate.
• the aforementioned chromium (CrM complex, iron (Fe) compound, yttrium (Y) compound, lanthanum (La) compound, cerium (Ce) compound, Ta Ngsten (W) compound, zirconium (Zr) compound, titanium (Ti) compound, vanadium (V) compound, phosphorus (P) compound, aluminum (A1) compound and molybdenum (Mo) compound A catalyst containing a homogeneous catalyst which is contained in the reaction solution and an amine compound (amine-compound combination type) is also preferably mentioned.
• the above amine compound is not particularly limited as long as it is a compound having an amine functional group in the molecule, and specifically, cyclic amines such as trialkylamines and pyridine and quaternary salts thereof. And homogeneous amines.
• the catalytic activity can be synergistically improved, and the reaction conversion rate and reaction selectivity can be increased at any rate.
• the amount of the catalyst used in the production method of the present invention is not limited, but, for example, a homogeneous system soluble in the reaction solution, containing at least one selected from the group consisting of chromium (Cr) compounds described above.
• a catalyst in which an amine compound is not used in combination, type
• the amount of use of the amine compound is made to be 0.10 to L0 mole% relative to (meth) acrylic acid. Preferably from 0.02 to 5 moles. / 0 , more preferably 0.004 to 3 mol%. Chromium (Cr) conversion
• the use amount of the homogeneous catalyst containing at least one member selected from the group consisting of compound isotropy and soluble in the reaction solution is preferably 0.01-5 mol%, more preferably 0. . 02-5 mole 0/0, more preferably from 0.04 to 3 mol 0/0. When the amount is less than 0.01 mole 0/0, there is a possibility that a synergistic effect is not obtained, exceeds 5 mol%, there is a possibility that production cost is high.
• the reaction of (meth) acrylic acid with alkylene oxide may be a batch reaction (batch reaction) or continuous reaction.
• the reaction continuous reaction
• the continuous reaction which is preferred because it is economical and not necessary, is the reactor occupancy time, such as raw material charging, heating, cooling, extraction and standby, as in the batch reaction. It is preferred because it can increase productivity because there is no
• the reaction is allowed to proceed by appropriately supplying the catalyst, (meth) acrylic acid and alkylene oxide to the reactor as appropriate. It is general to terminate the reaction when the amount of residual (meth) acrylic acid in the reaction reaches the desired amount.
• the reaction between (meth) acrylic acid and alkylene oxide is an exothermic reaction, and the reaction starts when the raw material compounds coexist in the presence of a catalyst in the reactor, and the reaction is caused by cooling or the like.
• the reaction can be terminated by lowering the temperature of the reaction solution in the vessel below a predetermined reaction temperature.
• the (meth) acrylic acid and the method for supplying the alkylene oxide generally include only (meth) acrylic acid in the reactor or a part thereof.
• the supply of (meth) acrylic acid and alkylene oxide may be either batch addition or sequential addition (continuous addition and Z or intermittent addition), but it is preferable. After that, it is better to put in bulk for the initial preparation It is good to put in one by one about what is supplied to.
• continuous charging means a mode in which the charging is performed a little bit continuously
• intermittent charging means a mode in which the charging is performed in an arbitrary number of times in a pulsed or intermittent manner.
• the feeding speed may be kept constant while advancing to the feeding end, or the speed may be changed at least once on the way, or the speed itself may be continuously The progress may be made while making changes as needed. However, if you want to change the speed on the way, it is preferable to reduce the speed before and after the change.
• alkylene oxide When alkylene oxide is continuously fed, in order to control the reaction temperature, the injection rate is changed to be increased halfway (ie, the speed is increased from before change to after change). Method is also preferably mentioned.
• alkylene oxide is continuously introduced at a liquid temperature which is lower than the set temperature by a predetermined temperature (for example, 1 ° C.), and control of the set temperature is facilitated by raising the liquid temperature by the heat of reaction. The method is also preferably mentioned.
• reaction solution is evaporated on the wall surface of the reactor and the vapor phase part of the distillation column, and the polymerization inhibitor condensed on the wall surface of the vapor phase part does not contain the (meth) acrylic acid and hydroxyalkyl (meth) Since there is a problem that a polymer is generated when the atarilate is thermally retained, it is preferable to wash and flow the condensate (including the polymer) with a reaction solution containing a polymerization inhibitor described later. ,.
• the time required to complete the supply of all the (meth) acrylic acid and alkylene oxide is not limited, and considering the progress of the reaction, the production cost, etc. It should be set.
• the catalyst the (meth) acrylic acid and the alkylene oxide are continuously supplied to the reactor to cause the reaction to proceed, thereby allowing the reaction to proceed. It is general to withdraw the reaction liquid from the reactor to complete the reaction when the residence time for the amount of (meth) acrylic acid remaining in the liquid reaches a desired amount.
• the reaction between (meth) acrylic acid and alkylene oxide is an exothermic reaction, and the above reaction starts from the time when these starting compounds are continuously introduced into the reactor and coexist in the presence of a catalyst, The reaction can be terminated by setting the temperature of the reaction solution continuously withdrawn to a temperature lower than a predetermined reaction temperature set by cooling or the like.
• the supply method (supply order, supply amount, etc.) of (meth) acrylic acid and alkylene oxide generally includes the total amount of (meth) acrylic acid and the alkylene group in the reactor.
• the ability to simultaneously supply the total amount of oxids is not limited to this.
• (meth) acrylic acid and alkylene oxide may be added to each reactor. It may be divided and supplied, and only (meth) acrylic acid may be dividedly supplied to each reactor.
• reaction When the reaction is carried out by a continuous reaction, it is preferable to continuously feed the (meth) acrylic acid and the alkylene oxide while keeping the feeding rate constant, even though it is better to feed them sequentially. .
• the production method of the present invention is carried out either by batch reaction or continuous reaction (hereinafter referred to as "batch reaction 'carried out by continuous reaction"), (meth) acrylic.
• the acid or alkylene oxide may be introduced into the reactor at normal temperature, or it may be preheated to a desired temperature so as not to change the temperature of the reaction solution at that time. You can throw it in!
• the reaction temperature is generally preferably in the range of 40 to 130 ° C, more preferably 50 to 100 ° C. If the reaction temperature is less than 40 ° C., the progress of the reaction may be delayed and the practicability may be lost, and if it exceeds 130 ° C., (meth) acrylic acid and the desired product, which are raw materials, are used. As a result of the polymerization of certain hydroxyalkyl (meth) phthalates, the amount of by-products formed may increase.
• the pressure in the system during the reaction generally depends on the kind and mixing ratio of the raw material compounds to be used, but in general, it is preferable to be under pressure.
• a reaction solvent may be used for the purpose of promoting the reaction mildly.
• the reaction solvent is not limited, but common solvents such as toluene, xylene, heptane and octane can be used.
• the above reaction (batch reaction or continuous reaction) and distillation can be carried out in the presence of a polymerization inhibitor.
• a polymerization inhibitor generally known ones can be used, but are not limited thereto.
• hydroquinone, methyl hydroquinone, tert butyl hydroquinone, 2,6 di tert butyl hydroquinone, 2,5 di tert butyl hydroquinone, 2, 4 Phenyl compounds such as dimethyl 6-tert-butylphenol and hydroquinone monomethyl ether; N-isopropyl-N'-phenyl para-phenyl diphenamine, N- (1,3-dimethylbutyl) ⁇ '-phenyl-para Phase 1-radiamine, ⁇ -(1-methyl heptyl) ⁇ '- ⁇ ⁇ -1 ⁇ ⁇ ⁇ - ⁇ ⁇ ⁇ , ⁇ , ⁇ '- ⁇ ⁇ ⁇ 1-pha 1 ⁇ ⁇ ⁇ - ⁇ ⁇ ⁇ ⁇ ⁇ ⁇ , ⁇
• the polymerization inhibitor may be used alone or in combination of two or more.
• the amount of the polymerization inhibitor added is preferably 0.1 to 1% by weight based on the carboxylic acid.
• the amount is more preferably 0.000 to 0.5% by weight Since the polymerization inhibitor is usually added in excess at the time of reaction or distillation, the polymerization inhibitory effect may be lost due to partial deterioration or the like. However, since most of them have the effect of preventing polymerization, it is possible to reduce the amount of polymerization inhibitor used by recycling the reaction liquid from which the hydroxyalkyl (meth) atalylate is distilled off.
• the polymerization inhibitor may be added directly to the reactor or distillation column, and the reaction solution, hydroxyl (meth) atarylate, or reaction solution obtained by distilling hydroxyalkyl (meth) atarylate may be previously added. It may be dissolved and introduced at once or may be introduced one by one.
• acids may be used in combination with a polymerization inhibitor, as described in JP-A 2003-267 929, in order to enhance the effect of preventing polymerization.
• the desired product hydroxyalkyl (meth) atalylate is distilled off (distilled and purified) from the reaction solution after completion of the reaction.
• a distillation method using a general-purpose distillation column, a packed column, a bubble column, a perforated plate column or other rectification column can be adopted, but the method is not limited thereto.
• other purification means can be used in combination.
• the conditions for carrying out distillation purification are, specifically, for example, a vacuum degree of 1 to 50 hPa is preferable 1 to 20 hPa is more preferable 1 to 1: LO hPa is more preferable.
• the distillation temperature is preferably 50 to 120 ° C, more preferably 60 to 100 ° C.
• the distillation time is preferably 0.5 to 24 hours, more preferably 0.5 to 12 hours, still more preferably 1 to 6 hours, and particularly preferably 1 to 3 hours. Reaction of distilling off hydroxyalkyl (meth) atalylate It is preferable to keep the temperature below the distillation temperature for at least 5 days, as the liquid may cause deterioration of the liquid properties such as increase in viscosity and increase of by-products due to heat history due to temperature, time, etc. In the case of storage, the temperature is preferably maintained at 50 ° C. or less.
• the above-mentioned polymerization inhibitor can be appropriately used also in distillation and purification.
• the amount of catalyst used relative to the total amount of (meth) acrylic acid supplied is taken as the catalyst concentration, and the total amount of (meth) acrylic acid supplied is calculated.
• the catalyst concentration represented by the total amount used of the catalyst is 1, the reaction is started in the state exceeding the catalyst concentration force ⁇ (ie, the catalyst concentration at the start of the reaction is in the state of exceeding 1) 2.
• the manufacturing method is preferably applicable.
• the reaction start time is assumed to be when the temperature of the reaction system into which (meth) acrylic acid as a raw material and, if necessary, alkylene oxide has been added reaches 40 ° C. or higher.
• the time when the content of the component is less than 0.5% is defined as the end of the reaction.
• the catalyst concentration after the start of the reaction means that the catalyst was supplied at any time from the start of the reaction to the end of the reaction (meta) It is assumed that it is the ratio of the total usage of the catalyst introduced up to that point to the total metering of acrylic acid. It is preferable to start the reaction in a state where the catalyst concentration force ⁇ is exceeded as described above.
• the catalyst concentration exceeds 1.0 as much time as possible from the start of the reaction to the end of the reaction.
• the supply of the total amount of alkylene oxide is It is particularly preferred to set up the feed conditions of the raw material so that the supply of the total supply of (meth) acrylic acid ends at the same time as or after the end.
• the total supply time in which the temperature of the supplied material is 40 ° C. or higher is, in other words, the material supplied to the reactor so far (reaction liquid) When the alkylene oxide and Z or (meth) acrylic acid are supplied into the reactor when the temperature power of the solution is higher than o ° c, the total time required for the supply (alkylene oxide and (meth) When there is a time to supply both acrylic acid and a time to supply only one, it is the total time).
• the time required for the supply is also the total supply time at which the temperature of the supplied raw material is 40 ° C. or higher. Is included in
• the adjustment of the molar ratio (alkylene oxide Z (meth) acrylic acid) within the above range is due to the fact that the temperature of the supplied raw material is 40 ° C. or higher during the time required for supplying both raw materials. It is more preferable to set it for 60% or more of the total supply time, and more preferably for the total supply time for which the temperature of the supplied raw material is 40 ° C. or more. In addition, even if the temperature of the supplied raw material is less than 40 ° C., it is more preferable to adjust the molar ratio (alkylene oxide Z (meth) acrylic acid) to be in the above range.
• the molar ratio (alkylene oxide) is 40% or more, preferably 60% or more, more preferably 100% of the total feed time when the temperature of the fed raw material is 20 ° C. or higher. It is most preferable to adjust the ratio of (meth) acrylic acid) to the above range, and in the form, coexistence of the catalyst, (meth) acrylic acid and alkylene oxide in the reactor. From the point of time of absence, it is preferable to adjust the molar ratio (alkylene oxide Z (meth) acrylic acid) within the above range.
• the above-mentioned molar ratio (alkylene oxide Z (meth) acrylic acid) is the specific time described above. There is no particular limitation as long as it is a charging method exceeding 1.0, but in order to effectively suppress diadducts (and even triad adducts, etc.), (meth) acrylic acid is added to the reactor. Part of acid or Preferably, the entire amount is initially charged, to which alkylene oxide or alkylene oxide and the remainder of (meth) acrylic acid are supplied.
• the molar ratio of the total amount of (meth) acrylic acid and the total amount of alkylene oxide (in the alkylene oxide (meth) acrylic acid) charged into the reactor is 1.
• the sum of the total amount of (meth) acrylic acid and the total amount of alkylene oxide introduced into the reactor so far during that step is supplied by the end of the reaction It is preferred that the total amount of (meth) acrylic acid and the total amount of alkylene oxide be 60% by weight or less.
• the total force of the total amount of (meth) acrylic acid and the total amount of alkylene oxide which has been charged into the reactor so far by the end of the reaction total feed amount of (meth) acrylic acid and alkylene make it 50% by weight or less with respect to the total of the total supply of oxide.
• the diester body is relatively likely to be by-produced, but (meth) acrylic acid and alkylene oxide at that stage
• a production method when batch reaction is carried out, a production method can be preferably applied in which the operation of purging the reaction gas containing alkoxide present in the reactor is carried out during the reaction.
• this production method it is possible to efficiently suppress byproducts of the alkylene glycol di (meth) atalylate and dialkylene glycol mono (meth) acrylate which are impurities in the Notch reaction system, and furthermore, the reaction Can be made to require no special high pressure resistance.
• gas purge for example, there is a method of emitting alkylene oxide by gas purging the reaction gas in the reactor into an apparatus (eg, a distillation column etc.) kept at reduced pressure.
• the reaction gas may be appropriately purged during the reaction, and in particular, in order to efficiently suppress by-products of the diol body and the diadduct, the total (meth) acrylic acid supplied may be used.
• the reaction is carried out when the reaction conversion rate of the acid reaches 50% or more. It is preferable to carry out when the reaction conversion rate of total (meth) acrylic acid reaches 90% or more. If the reaction gas is purged when the reaction conversion of the total (meth) acrylic acid supplied is less than 50%, the reaction yield decreases and, at the same time, the remaining acid component increases and the acid component Since it is difficult to remove by purification such as distillation, there is a possibility that the product purity may decrease.
• the internal pressure is 80% of the pressure limit of the reactor, for the purpose of keeping the maximum ultimate pressure exerted on the reactor low and making the reaction in the low pressure resistant (for example, less than 1.OMPa) reactor possible.
• the reaction gas may be purged when it preferably exceeds 50%.
• the purge of the reaction gas may be performed continuously so as to be a constant pressure, may be performed once, or may be performed a plurality of times.
• To purge the reaction gas containing alkylene oxide present in the reactor means to remove gas components (gas) present in the gas phase in the reactor to the outside of the reactor.
• the specific operation method is not particularly limited. For example, when the reaction is carried out under pressure, the pressure in the reactor is released, and if the pressure in the reactor is reduced. In the case where nitrogen gas or inert gas (such as helium gas) is flowed into the reactor, the gas phase in the reactor is replaced with these gases. Alternatively, the pressure in the reactor may be reduced. In the present invention, in particular, the reaction is carried out under pressure, and the pressure in the reactor is determined by the reason that reaction under pressure is preferable, the operation for purging reaction gas is simple, and the like. Preferred is a form in which the reaction gas is purged by releasing it.
• the reaction gas When the reaction gas is to be purged, it is necessary to purge all the reaction gas in the reactor. Types of raw materials to be used and their proportions, pressure resistance of the reactor used, progress of reaction Depending on the situation, at least a portion of the reaction gas present in the reactor may be purged. Specifically, for example, for the purpose of efficiently suppressing by-products of diester and di-adduct, the concentration of alkylene oxide gas in the reaction gas present in the reactor is 60% by volume or less, preferably 50% by volume. In the following, it is preferable to determine the gas purge amount so as to be 40% by volume or less more preferably, for the purpose of suppressing the maximum ultimate pressure exerted on the reactor and reducing the pressure resistance. The internal pressure of the reactor is 60% or less, preferably 50% or less, relative to the desired maximum ultimate pressure absolute pressure. It is preferable to determine the gas purge amount so as to be 40% or less more preferably.
• the reaction can be made by judging when the remaining unreacted (meth) acrylic acid has sufficiently disappeared.
• the unreacted (meth) It is preferable to start cooling when the amount of acrylic acid is 0.2% by weight or less, preferably 0.1% by weight or less.
• the start of cooling may be either before or after the reaction gas is purged, or may be simultaneous.
• the amount of the acid component relative to the amount of the catalyst in the reaction solution is calculated to be from 0.010 to 100 in molar ratio.
• the reaction solution after distilling off the hydroxyalkyl (meth) acrylate is preferably used for the next reaction while maintaining the
• the state in which the amount of the acid component in the reaction liquid is not less than 0.010 and not more than 100 in molar ratio as described above with respect to the amount of catalyst in the reaction liquid is calculated. It is preferable to maintain the ratio, but the molar ratio is more preferably 0.03 or more and 50 or less, still more preferably 0.05 or more and 30 or less.
• the catalyst in the reaction solution becomes inactive, and even if the reaction solution after evaporation of hydroxyalkyl (meth) atalylate is used for the next reaction, There is a possibility that the catalyst activity may not be sufficiently exhibited.
• the value of the molar ratio is the ratio of molar concentration (mol%), that is, the ratio of molar concentration of acid component in the reaction liquid (mol%) to molar concentration of the catalyst in the reaction liquid (mol%). It is the same as
• the amount of the acid component in the reaction liquid may be the strength of (meth) acrylic acid, which is a raw material mixture, and other acids as described later.
• the reaction solution after evaporation of the hydroxyalkyl (meth) atalylate is used for the next reaction, It means maintaining the above molar ratio all the time until the next reaction is actually started (hereinafter sometimes referred to as a maintenance period).
• the above “calculation” means that the amount of catalyst in the reaction liquid is the amount of catalyst present in the reaction liquid at any time within the maintenance period. . Specifically, in the case of a batch reaction, it means the total amount of catalyst supplied to the reaction solution up to that point, and in the case of a continuous reaction, it means (if it is the reaction solution after removing reactor power). It means the amount converted from the catalyst concentration in the reaction solution in the reactor at the time of removal of the reactor).
• the amount of the acid component in the reaction liquid the amount of the acid component such as (meth) acrylic acid is present at any time in the reaction liquid in the reactor. Shall be meant.
• (meth) acrylic acid it is necessary to consider that it is consumed as the reaction proceeds because it is a starting compound for the reaction, but specifically, a part of the reaction solution at any of the above points is sampled Then, neutralization titration is performed to measure the concentration of the acid component in the reaction solution, and this value is converted to a value.
• (Meta) A means of supplying other acid such as acid, which is less reactive than acrylic acid, into the reaction liquid, and (iii) removing unreacted alkylene oxide from the reaction liquid simultaneously with the completion of the reaction (for example, gas purge or Gv) a means for decreasing the reaction temperature at the end of the reaction by 5 ° C. or more than the set temperature or a means for shortening the cooling time at the end of the reaction.
• the amount of acid components etc. in the reaction liquid may be controlled sequentially as the reaction proceeds, as needed).
• Examples of the above-mentioned low reactivity !, acid include carboxylic acids of 6 or more carbon atoms such as octanoic acid, isooctanoic acid, decanoic acid, dodecanoic acid and the like, and saturated carboxylic acids.
• the first method is applicable to all known or already proposed methods for producing hydroxyalkyl (meth) atarylates by reaction of (meth) acrylic acid with alkylene oxide.
• the present invention can be preferably applied to a production method in which the molar specific force of alkylene oxide relative to (meth) acrylic acid initially charged is equal to or greater than ⁇ .
• This manufacturing method In the method, when the molar ratio at the time of initial charging is, for example, 1.4 or more, there has been a problem that catalyst inactivity is significant, but the first method is applied. If the molar ratio of the amount of the acid component to the amount of the catalyst in the reaction solution is maintained to satisfy the above-mentioned range, the above problems can be easily solved. This is that when the molar ratio at the time of initial charging is large, the molar ratio of the amount of the acid component to the amount of the catalyst in the reaction liquid may fall below the molar ratio in the first method during the reaction. It is thought that the power that was
• reaction liquid after distilling off the desired product hydroxyalkyl (meth) atalylate is used for the next reaction, and the catalyst used for the reaction is again used in the same manner.
• reaction liquid after the distillation the reaction liquid after completely reacting (meth) acrylic acid, which is a raw material compound, with an alkylene oxide and carrying out the above distillation may be used.
• the reaction solution after the reaction is completed and the above-mentioned distillation is completed at any stage during the reaction of (meth) acrylic acid and alkylene oxide, and the recycling efficiency of the catalyst and the desired product are not limited. It may be selected appropriately in consideration of further improving the yield etc. of
• the target product hydroxyalkyl (meth) atalylate may be completely distilled off, or may be partially distilled off. It may remain without being limited.
• other by-products and other components such as raw materials and the like may remain in the reaction solution after the above distillation, and may be distilled off together with the target product.
• the reaction solution is used for the next reaction in the state where the di adduct of alkylene oxide (dialkylene glycol mono (meth) atalylate) as a by-product is left.
• byproducts of the diadduct can be effectively suppressed.
• dialkylene glycol mono (meth) atalylate is supplied into the reaction system, and dialkylene glycol mono (meta It is important to keep the atarilate (diadduct) coexist.
• the amount of the diadduct to be allowed to coexist is preferably in a molar ratio of 2 to: LOO as calculated relative to the amount of catalyst in the reaction solution, more preferably 5 to 80, More preferably, it is 5 to 60, and particularly preferably 5 to 40. If the molar ratio is less than 2, the inhibitory effect of the diadduct may not be obtained. If it exceeds 100, although the inhibitory effect of the diadduct is effective, the absolute amount in the reaction solution increases and Rate and purity may be reduced.
• the above “in calculation” means that the amount of catalyst in the reaction liquid is the amount of catalyst present in the reaction liquid at any time before or during the reaction. Do. Specifically, in the case of a batch reaction, it means the total amount of catalyst supplied to the reaction liquid up to that point, and in the case of a continuous reaction, the catalyst concentration power in the reaction liquid in the reactor at that point It shall mean the amount to be converted.
• the amount of catalyst in the reaction solution it is necessary to determine whether the catalyst performance originally inherent in the reaction has been reduced or eliminated, or the catalyst performance has originally been eliminated. Do not take into consideration whether or not
• the mode of supplying dialkylene glycol mono (meth) atalylate into the reaction system is not particularly limited.
• the reaction of (meth) acrylic acid and alkylene oxide It may be supplied in advance, or may be supplied to the reaction solution during the reaction of (meth) acrylic acid and alkylene oxide, but preferably before reaction of (meth) acrylic acid and alkylene oxide. It is an aspect supplied beforehand. By thus pre-feeding before the reaction, it is possible to obtain a higher effect of suppressing the formation of the diadduct.
• the diadducts supplied in advance before the reaction may be all or a part thereof (in the case of one part, the rest is supplied to the reaction solution during the reaction), and the limitation is Although not preferred, all are more preferred, with more preferred.
• the source of the diadduct supplied into the reaction system is not limited, but in general, the desired product hydroxyalkyl (meth) atalylate is distilled off in the same reaction as described above. It is preferable to use a reaction solution after removal which contains the diadduct formed in the previous reaction. That is, it is preferable to use the dialkylene glycol mono (meth) atarelate contained in the reaction solution after distilling off the hydroxyalkyl (meth) atalylate to supply the reaction system. In this embodiment, the remaining reaction solution is It can be reused effectively. In addition, since the residual reaction solution also contains the catalyst used for the reaction, the catalyst can be used again for the same reaction (recycled), which is preferable.
• the reaction liquid after the above evaporation As the reaction liquid after the above evaporation, the (meth) acrylic acid, which is a mixture of raw materials in the above reaction, is completely reacted with the alkylene oxide to carry out the above evaporation. Even if the reaction solution is used, the reaction solution may be used after the reaction is completed and the above-mentioned distillation is performed at any stage during the reaction of (meth) acrylic acid and alkylene oxide. However, it may be selected appropriately in order to further improve the recycling efficiency of the catalyst and the yield of the desired product. In the reaction liquid after the above distillation, the desired product, hydroxyalkyl (meth) atalylate, may be completely distilled off, or may be partially left without being distilled off. There is no limitation.
• the second method it is preferable to use the whole amount of the reaction solution after distilling off the desired product after reaction for the next reaction, but the method is not limited. Only part of the reaction may be used, or it may be divided and used in multiple reactions.
• the first method of the above-mentioned production methods of the present invention can be preferably applied. The specific aspect of the first method is as described above.
• a production method in which the molar ratio of alkylene oxide to (meth) acrylic acid initially charged is 1 or more can be preferably applied.
• the problem is that catalyst inactivity is significant. If the molar ratio of the amount of the acid component to the amount of the catalyst in the reaction solution is maintained so as to satisfy the above-mentioned range, the above problems can be easily solved. This is that when the molar ratio at the time of initial charging is large, the molar ratio of the amount of the acid component to the amount of the catalyst in the reaction liquid falls below the molar ratio in the first method during the reaction. It is considered to be a force that
• the reaction liquid supplemented with the novel catalyst is used for the next reaction by distilling off the hydroxyalkyl (meth) atalylate. Specifically, after the target product is distilled off from the reaction solution, the spent catalyst is recovered as it is, and the recovered solution is supplemented with a new catalyst, and reused in the next reaction. Ah Ru.
• this production method the amount of catalyst used is greatly reduced, and at the same time, a high catalyst recovery rate ensuring low cost, excellent economy, easy operation and easy catalyst reuse, and sufficient catalytic reaction are obtained. Efficiency can be achieved.
• a catalyst in a reaction solution (hereinafter, may be referred to as a residual reaction solution) containing a catalyst used for the reaction after the target product is distilled off, and a catalyst newly replenished (hereinafter, new)
• a catalyst comprising the catalyst hereinafter sometimes referred to as “catalyst”
• the new catalyst is dissolved in the remaining reaction solution in advance.
• a new catalyst may be dissolved in the remaining reaction solution after the next reaction starts, or a new reaction may be previously added to the remaining reaction solution.
• the reaction solution may be added after the next reaction has started, especially if the reaction takes place.
• the entire amount of the new catalyst to be replenished is previously dissolved in the total amount of the remaining reaction solution to be used in the next reaction, and then it is used in the next reaction. It is easy to handle as a catalyst used for the next reaction without being complicated.
• the novel catalyst is preferably the same as the catalyst that can be used in the production method of the present invention listed above.
• the residual reaction solution is a solution obtained by distilling off the desired product hydroxyalkyl (meth) atalilate from the solution after reaction, and the desired product is not completely distilled off, and remains somewhat. Do not mind,.
• the remaining reaction solution may be used for the next reaction as a whole, or only a part may be used, or it may be arbitrarily divided and used in a plurality of reactions. There is no limitation as long as at least a part of the catalyst can be used again as a reaction catalyst.
• a portion of the remaining reaction solution preferably 20 to 90% by weight, more preferably 30 to 80% by weight, still more preferably 40 to 80% by weight, particularly preferably 50 to 80% by weight. It recycles to the reaction system of the above, and the form which discards the remainder of the remaining reaction liquid is mentioned.
• the amount of replenishment of the new catalyst is necessary for the reaction system when the catalyst in the remaining reaction liquid to be recycled is completely inactivated when the entire amount of the above remaining reaction liquid is used for the next reaction. It is preferable to replenish 100% by weight of the catalyst amount.
• the catalyst in the remaining reaction solution to be recycled is lost. If it is not active and 100% by weight of the catalyst necessary for the reaction system can be provided, it may not be replenished.
• Ethylene oxide is supplied for 0.7 hours at 136 g Zh (94 g), after which acrylic acid (280 g) at 215 g Zh and ethylene glycol (178 g) at 136 g Zh are supplied for 1.3 hours, during which 85 ° C. Maintained to react.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as acrylic acid (measured by the titration with sodium nitrate) became 0.10 wt%.
• the concentration of the acid component at the point when the reaction was continued for 1 hour was 0. 10 ⁇ %, so the reaction solution was cooled to 30 ° C or less in 10 minutes (the reaction duration was finally reached 1. It was 2 hours).
• the acid component of the obtained reaction solution was 0.05 wt% (molar ratio of acid component to catalyst: 0. 07).
• reaction solution was depressurized to a vacuum degree of 4 hPa, and the obtained reaction solution was also transferred by pressure transfer to the above flask.
• the unreacted ethylene oxide was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Z min.
• the acid component of the obtained reaction solution was 0.05 wt% (molar ratio of acid component to catalyst: 0. 07).
• the reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxylatarylate was distilled off.
• Acid of reaction liquid obtained The composition was 0.05 wt% (molar ratio of acid component to catalyst: 0. 07).
• the reaction liquid 69.5 g obtained by evaporating the above-mentioned hydroxyl atalylate and the 70.5 g portion of the total supply amount of 380 g of acrylic acid are charged in a 1-liter SUS316 autoclave equipped with a stirrer, After replacing with nitrogen gas, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic ethylene was supplied for 0.4 hours at 123 g Zh (47.5 g), then acrylic acid (309.5 g) at 193.5 g / h, ethylene oxide (198.5 g) at 123 g Zh, The reaction was carried out while maintaining the temperature at 85 ° C. for the time.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide is kept constant at 85 ° C, and the reaction is continued until the concentration of the acid component as acrylic acid (measured by neutralization titration) reaches 0.10 wt%.
• the concentration of the acid component became 0.10 wt ° / ( ⁇ ) by continuing the reaction for 1.3 hours.
• Example 1-1 0.5 g of octanoic acid was charged into a 1 L glass round bottom flask set in a vacuum distillation apparatus, the vacuum degree was reduced to 4 hPa, and the resulting reaction solution was also transferred to the above flask by pressure transfer. It carried out like Example 1-1. Unreacted ethylene oxide was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Zmin in the same manner as in Example 1-1. The acid component of the resulting reaction solution was 0.06 wt% (molar ratio of acid component to catalyst: 0.88). Thereafter, the reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxylatarylate was distilled off. The acid component of the obtained reaction solution was 0.06 wt% (molar ratio of acid component to catalyst: 0.88).
• the reaction liquid 69.5 g obtained by evaporating the above-mentioned hydroxyl atalylate and the 70.5 g portion of the total supply amount of 380 g of acrylic acid are charged in a 1-liter SUS316 autoclave equipped with a stirrer, After replacing with nitrogen gas, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic ethylene was supplied for 0.4 hours at 123 g Zh (47.5 g), then acrylic acid (309.5 g) at 193.5 g / h, ethylene oxide (198.5 g) at 123 g Zh, The reaction was carried out while maintaining the temperature at 85 ° C. for the time.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as acrylic acid (measured by the titration with sodium nitrate) became 0.10 wt%. By the way, the concentration of the acid component at the point when the reaction was continued for 0.85 hours became 0.10 ⁇ %, so the reaction solution was cooled to 30 ° C. or less in 30 minutes (the reaction duration was finally reached 1. It was 05 hours).
• the acid component of the reaction solution obtained was 0.0005 wt% (molar ratio of acid component to catalyst: 0.00 007)
• the resulting reaction solution was pressure transferred to a 1 L glass round bottom flask set in a vacuum distillation apparatus. Unreacted ethylene oxide was dissipated at a vacuum level of 4 hPa and an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Z min.
• the acid component of the resulting reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.007).
• the reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxylatarylate was distilled off.
• the acid component of the resulting reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.007).
• the reaction liquid 69.5 g obtained by evaporating the above-mentioned hydroxyl atalylate and the 70.5 g portion of the total supply amount of 380 g of acrylic acid are charged in a 1-liter SUS316 autoclave equipped with a stirrer, After replacing with nitrogen gas, the temperature is raised to 85 ° C, and the internal pressure is 0.05MPa (G) And Acidic ethylene was supplied for 0.4 hours at 123 g Zh (47.5 g), then acrylic acid (309.5 g) at 193.5 g / h, ethylene oxide (198.5 g) at 123 g Zh, The reaction was carried out while maintaining the temperature at 85 ° C. for the time.
• reaction liquid 69.5 g from which the above-mentioned hydroxypropyl atalylate has been distilled off and 57.5 g of the total supply of 342 g of acrylic acid are charged into a 1 l capacity SUS 316 autoclave equipped with a stirrer, and the inside of nitrogen is charged. After gas substitution, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic propylene is supplied at 0.14 hours at 142 g / h (51 g), then acrylic acid (284.5 g) at 173.5 g / h, propylene oxide (232.5 g) at 142 g Zh, 1 The reaction was carried out while maintaining the temperature at 85 ° C. for 6 hours.
• a 1-liter glass round bottom flask set in a vacuum distillation apparatus was depressurized to a vacuum level of 4 hPa, and the obtained reaction solution was transferred by pressure transfer to the above-described flask.
• the unreacted propylene oxide was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Z min.
• the acid component of the obtained reaction solution was 0.04 wt% (molar ratio of acid component to catalyst: 0.06).
• the reaction product was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxy propyl aralilate was distilled off.
• the acid component of the obtained reaction solution was 0.04 wt% (molar ratio of acid component to catalyst: 0.06).
• reaction liquid 69.5 g from which the above-mentioned hydroxypropyl atalylate has been distilled off and 57.5 g of the total supply of 342 g of acrylic acid are charged into a 1 l capacity SUS 316 autoclave equipped with a stirrer, and the inside of nitrogen is charged. After gas substitution, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic propylene is supplied at 0.14 hours at 142 g / h (51 g), then acrylic acid (284.5 g) at 173.5 g / h, propylene oxide (232.5 g) at 142 g Zh, 1 The reaction was carried out while maintaining the temperature at 85 ° C. for 6 hours.
• the reaction temperature after the completion of the supply of acrylic acid and propylene oxide is kept constant at 85 ° C., and the concentration of the acid component as acrylic acid (by neutralization titration) The reaction was continued until the measurement became 0.10 wt%. By continuing the reaction for 1.5 hours, the concentration of the acid component became 0.10 wt ° / ( ⁇ ).
• reaction temperature constant at 85 ° C after the completion of the supply of phthalic acid and propylene acid, and continue the reaction until the concentration of the acid component as acrylic acid (measured by neutralization titration) reaches 0.10 wt%.
• the reaction solution was cooled to 30 ° C. or less in 30 minutes because the concentration of the acid component reached 0.1 wt% when the reaction was continued for 4 hours. Finally it was 1.6 hours).
• the acid component of the obtained reaction solution was 0.0005 wt% (monolithic ratio of acid component to catalyst: 0.008).
• reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.008).
• reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution obtained by evaporating hydroxypropyl atalylate.
• the acid component of the resulting reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.008).
• reaction liquid 69.5 g from which the above-mentioned hydroxypropyl atalylate has been distilled off and 57.5 g of the total supply of 342 g of acrylic acid are charged into a 1 l capacity SUS 316 autoclave equipped with a stirrer, and the inside of nitrogen is charged. After gas substitution, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic propylene is supplied at 145 g / h for 0.4 hours (51 g) and then 173.5 g / h The acrylic acid (284.
• reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.008).
• reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution obtained by evaporating hydroxypropyl atalylate.
• the acid component of the resulting reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.008).
• reaction liquid 69.5 g from which the above-mentioned hydroxypropyl atalylate has been distilled off and 57.5 g of the total supply of 342 g of acrylic acid are charged into a 1 l capacity SUS 316 autoclave equipped with a stirrer, and the inside of nitrogen is charged. After gas substitution, the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G). Acidic propylene is supplied at 0.14 hours at 142 g / h (51 g), then acrylic acid (284.5 g) at 173.5 g / h, propylene oxide (232.5 g) at 142 g Zh, 1 The reaction was carried out while maintaining the temperature at 85 ° C. for 6 hours.
• the mixture was charged into a SUS316 autoclave and replaced with nitrogen gas, and then the temperature was raised to 85 ° C., and the internal pressure was adjusted to 0.05 MPa (G).
• the reaction temperature was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as methacrylic acid (measured by neutralization titration) was 0.10 wt%.
• concentration of the acid component at the point of continuing the reaction was 0.10 wt%
• the reaction solution was cooled to 30.degree. C. or less in 10 minutes (the reaction duration was finally 1.8 hours).
• the acid component of the resulting reaction solution was 0.003 wt% (molar ratio of acid component to catalyst: 0.33).
• reaction solution was depressurized to a vacuum degree of 4 hPa, and the obtained reaction solution was also transferred by pressure to the above flask.
• the unreacted oxidized propylene was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Zmin.
• the acid component of the obtained reaction solution was 0.003 wt% (molar ratio of acid component to catalyst: 0.33).
• the reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxypropyl methacrylate was distilled off.
• the acid component of the obtained reaction solution was 0.003 wt% (molar ratio of acid component to catalyst: 0.33).
• the reaction temperature is kept constant at 85 ° C. until the concentration of the acid component as methacrylic acid (measured by neutralization titration) reaches 0.10 wt%.
• the concentration of the acid component became 0.1 Owt ° / ⁇ by continuing the reaction for 1. 6 hours.
• the reaction temperature was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as methacrylic acid (measured by neutralization titration) was 0.10 wt%.
• concentration of the acid component at the point when the reaction was continued for 0.6 hours was 0.10 wt%, so the reaction solution was cooled to 30 ° C. or less in 30 minutes (the reaction duration was finally 1. 8 hours).
• the acid component of the obtained reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.006).
• reaction solution was depressurized to a vacuum degree of 4 hPa, and the obtained reaction solution was also transferred by pressure to the flask.
• the unreacted oxidized propylene was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Zmin.
• the acid component of the resulting reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.006).
• the reaction solution was purified by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 69.5 g of a reaction solution from which hydroxypropyl methacrylate was distilled off.
• the acid component of the obtained reaction solution was 0.0005 wt% (molar ratio of acid component to catalyst: 0.006).
• the reaction temperature is kept constant at 85 ° C., and the concentration of the acid component as methacrylic acid (measured by neutralization titration) is 0.1% by weight.
• the concentration of the acid component became 0.1 Owt ° / ⁇ by continuing the reaction for 1.8 hours.
• Ethylene oxide is supplied for 10 minutes at 218 g Zh (36 g), and then acrylic acid (634 g) at 328 g Zh and ethylene oxide (400 g) at 218 g Zh are supplied for 110 minutes while reacting at 85 ° C.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide is kept constant at 85 ° C.
• the reaction was continued until the concentration of the solution (measured by neutralization titration) was 0.10 wt%, but the concentration of the acid component became 0.10 wt% when the reaction was continued for 60 minutes. Therefore, the reaction solution was cooled to room temperature (the reaction duration was finally 70 minutes).
• the reaction solution obtained was analyzed by gas chromatography to find that the diethylene glycol monoatalylate concentration was 8.5 wt% (0. 716 mol), and therefore, diethylene glycol monoatarylate newly formed during the reaction was obtained.
• the concentration was found to be 3. 75 wt% (0. 316 mol) (acrylic acid based diethylene glycol monoatalylate selectivity: 3.3 mol%;).
• Ethylene oxide is supplied for 45 minutes at 264 g Zh (198 g), and then acrylic acid (589 g) at 471 g Zh and ethylene glycol (329 g) at 264 g Zh are supplied for 75 minutes, while maintaining the temperature at 85 ° C. I did.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide is kept constant at 85 ° C, and the reaction is continued until the concentration of the acid component as acrylic acid (measured by neutralization titration) reaches 0.10 wt%.
• the concentration of the acid component at the point of continuing the reaction was 0.10 wt ° / ( ⁇ , so the reaction solution was cooled to room temperature (the reaction duration was 80 minutes at the end) ).
• the reaction liquid obtained was analyzed by gas chromatography, and it was found that the concentration of diethylene glycol monoallytalate newly generated during the reaction was 6.2 wt% (0.523 mol) (acrylic acid based diethylene glycol) mono Atari rate selectivity: 4.6 mol 0/0).
• Acidic ethylene is supplied at a rate of 221 g / h for 10 minutes (37 g), and thereafter acrylic acid (634 g) at a rate of 328 g / h and ethylene oxide (405 g) at 221 g Zh are supplied for 110 minutes.
• the reaction was performed while maintaining C.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as acrylic acid (measured by neutralization titration) was 0.10 wt%. However, the concentration of the acid component at the point when the reaction was continued for 65 minutes was 0.10 wt%, so the reaction solution was cooled to room temperature (the reaction duration was finally 75 minutes).
• the reaction liquid obtained was analyzed by gas chromatography to find that the diethylene glycol monoatalylate concentration was 6. Owt% (0.507 mol), and therefore, diethylene glycol monoatarylate newly formed during the reaction was obtained.
• the concentration was found to be 5.63 wt% (0. 476 mol) (acrylic acid based diethylene glycol monoarylate selectivity: 5.0 mol%;).
• a 1 L glass round bottom flask set in a vacuum distillation apparatus was depressurized to a vacuum level of 4 hPa, and lOOg of the reaction liquid obtained in Example 2-1 was transferred from the autoclave to the flask by pressure transfer. Unreacted ethylene oxide was dissipated at an internal temperature of 40 to 50 ° C. for 30 minutes while publishing air at 3 mL Z min. Thereafter, purification was carried out by distillation at an internal temperature of 50 to 90 ° C. for 3 hours to obtain 275 g of a reaction solution from which hydroxylatarylate was distilled off. The reaction solution obtained was analyzed by gas chromatography to find that the concentration of diethylene glycol monoazatalylate was 27.6 wt%.
• reaction liquid Diethylene dalchol mono atalylate: 27.6 wt% (0. 388 mol), chromium acetate: 3.3 g in calculation
• total supply of acrylic acid after distilling the above hydroxyl atarylate 48 g of 682 g, 1.7 g (0.020 mol) of chromium acetate as catalyst (molar ratio of diethylene glycol monoallylate to chromium acetate: 19), 0.42 g of phenothiazine as polymerization inhibitor
• After charging into a 2-liter stainless steel SUS316 autoclave and replacing the inside with nitrogen gas The temperature was raised to 85 ° C, and the internal pressure was set to 0.05MPa (G).
• the acid ethylene is supplied for 10 minutes at 218 g Zh (36 g), and thereafter acrylic acid (634 g) at 328 g Zh and ethylene oxide (400 g) at 218 g Zh are supplied for 110 minutes while maintaining 85 ° C. It was made to react.
• the reaction temperature after the completion of the supply of acrylic acid and ethylene oxide was kept constant at 85 ° C, and the reaction was continued until the concentration of the acid component as acrylic acid (measured by neutralization titration) was 0.10 wt%. However, the concentration of the acid component at the point when the reaction was continued for 60 minutes was 0.10 wt%, so the reaction solution was cooled to room temperature (the reaction duration was finally 70 minutes).
• the reaction solution thus obtained was analyzed by gas chromatography, and the diethylene glycol monoatalylate concentration was 8.4 wt% (0.07 mol). Therefore, diethylene glycol monoatarylate newly formed during this reaction was obtained. the concentration 3. 80 wt% was found to be (0.319 mol) (diethylene glycol Atari rate selectivity of acrylic acid based:. 3 4 mole 0/0).
• the production method of the present invention is suitable as a production method of hydroxyalkyl (meth) atalylate with high production cost. According to the present invention, it is possible to provide a process for producing hydroxyalkyl (meth) atarylates which can realize low production costs. Specifically, by making the catalyst used for the reaction efficient and recyclable to the next reaction with respect to the amount and activity of the reaction, etc., or the di-adduct as a by-product (dialkylene glycol mono (meth) atari) By making it possible to effectively suppress the formation of (rate), it is possible to easily provide a method for producing hydroxyalkyl (meth) atarylates which can realize low production costs.

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