Patent Application
20240067602
The present invention relates to a method for preparing an isocyanate compound.
Although xylylene diisocyanate (hereinafter, referred to as XDI) contains an aromatic ring in its molecule, it is classified into aliphatic isocyanate. XDI is a compound very useful for raw materials such as polyurethane-based materials, polyurea-based materials, or polyisocyanurate-based materials in the fields of chemical industry, resin industry, and paint industry.
Commonly, when synthesizing isocyanate compound, many side reactions are generated, and thus, it is prepared by a method of reacting with anhydrous hydrochloric acid or carbonic acid to form a salt of amine compound and reacting it with phosgene.
As an example, XDI is prepared by reacting xylylene diamine (hereinafter referred to as XDA) with anhydrous hydrochloric acid to form an amine-hydrochloride salt, and then reacting it with phosgene. More specifically, in the prior art, an isocyanate compound such as XDI was prepared by reacting a liquid raw amine, such as XDA-containing solution, with anhydrous hydrochloric acid to form XDA-HCl hydrochloride, heating it to a high temperature of at least 100° C. or more, and then charging gas phase phosgene to progress a gas-liquid reaction.
The reaction of forming the isocyanate compound is a representative endothermic reaction, continuous heating and maintenance of a high temperature are required during the reaction so as to increase the yield.
By the way, since isocyanate compound such as XDI generally has high reactivity of the amino group, many side reactions are generated during the phosgenation reaction, and the by-products formed through the side reactions have an influence on a process in which isocyanate compounds are applied as raw materials (for example, a process for producing a polyurethane resin), thereby causing deterioration in resin quality.
As explained above, due the need to maintain a high temperature during the preparation process of isocyanate compound, and the high reactivity of the prepared isocyanate compound, such as XDI, there is a growing concern about the formation of by-products or the occurrence of side reactions by the thermal denaturation of products, and thus, high load has been frequently generated even in the purification process.
Due to such problems, various attempts have been made in the past to suppress side reactions or by-product generations during the preparation of isocyanate compound, but effective technology has not yet been developed.
In addition, attempts have been made to recover and reuse compounds such as phosgene and hydrogen chloride from exhaust gas generated during the preparation process of isocyanate compound, but there is a limit in that the efficiency is lowered.
It is an object of the present invention to provide a method for preparing an isocyanate compound that can recover and reuse materials used in the reaction during the preparation of an isocyanate compound using phosgene, and can minimize thermal denaturation of a reaction product and formation of by-products.
According to one embodiment of the present invention, there is provided a method for preparing isocyanate compound, comprising:
Now, a method for preparing an isocyanate compound according to one embodiment of the present invention will be described.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terms used herein are for the purpose of describing specific embodiments only and is not intended to limit the scope of the invention.
The singular forms “a,” “an” and “the” used herein are intended to include plural forms, unless the context clearly indicates otherwise.
It should be understood that the terms “comprise,” “include”, “have”, etc. are used herein to specify the presence of stated feature, region, integer, step, action, element and/or component, but do not preclude the presence or addition of one or more other feature, region, integer, step, action, element, component and/or group.
While the present invention can be modified in various ways and take on various alternative forms, specific embodiments thereof are illustrated and described in detail below. However, it should be understood that there is no intent to limit the present invention to the particular forms disclosed, but on the contrary, the present invention covers all modifications, equivalents, and alternatives falling within the spirit and scope of the present invention.
In describing a position relationship, for example, when the position relationship is described as ‘upon˜’, ‘above˜’, ‘below˜’, and ‘next to˜’, one or more portions may be arranged between two other portions unless ‘just’ or ‘direct’ is used.
In describing a time relationship, for example, when the temporal order is described as ‘after˜’, ‘subsequent˜’, ‘next˜’, and ‘before˜’, a case which is not continuous may be included unless ‘just’ or ‘direct’ is used.
As used herein, the term “low boiling material” means a material having a boiling point lower than that of the isocyanate compound which is a target product according to the present invention, and the term “high boiling material” means a material having a boiling point higher than that of the isocyanate compound, which is a target product according to the present invention.
As used herein, the term “bottom” of the distillation column means an outlet through which the lower discharged products of the distillation column are discharged to the outside of the distillation column, the term “top” of the distillation column means an outlet through which the upper discharged products of the distillation column are discharged to the outside of the distillation column.
According to one embodiment of the present invention, there is provided a method for preparing isocyanate compound, comprising:
According to another embodiment of the present invention, there is provided a method for preparing isocyanate compound, comprising:
According to yet another embodiment of the present invention, there is provided a method for preparing isocyanate compound, further comprising:
During the preparation of an isocyanate compound using phosgene, exhaust gases containing phosgene, hydrogen chloride and the like are discharged during the main reaction and purification processes. In accordance with environmental regulations, the exhaust gases are discharged into the atmosphere after removal of harmful substances by post-treatment.
The present inventors have found, as a result of continuous research, that when the exhaust gases from all processes including the gas phase obtained in the degassing step are processed through the gas compression step and the distillation step under the above conditions, phosgene, hydrogen chloride and the like contained in the exhaust gases can be more effectively recovered, and the recovered compounds can be supplied to the steps in need thereof, thereby reducing costs and increasing process efficiencies.
Furthermore, inventors have found that the reaction step, the degassing step, the desolvation step, the low boiling material-removing step, and the high boiling material-removing step are progressed to prepare an isocyanate compound, especially when the above steps are progressed under the above temperature and pressure conditions, the thermal denaturation of a reaction product and the formation of by-products can be minimized, and a high-purity isocyanate compound can be obtained.
(Phosgene Reaction Step)
A phosgene reaction step is progressed in which a salt of amine compound and phosgene are reacted in the presence of a solvent to obtain a reaction product containing an isocyanate compound, the solvent, and unreacted phosgene.
According to one embodiment of the invention, the amine compound is preferably applied as a salt of the amine compound in order to suppress rapid reactions and side reactions between the amine compound and phosgene. For example, the salt of amine compound may be a hydrochloride or carbonic acid salt of the amine compound.
The salt of the amine compound may be prepared by reacting an amine compound with anhydrous hydrochloric acid or carbonic acid and performing a neutralization reaction. The neutralization reaction can be progressed at a temperature of 20 to 80° C.
The salt of the amine compound can be obtained by reacting the amine compound with anhydrous hydrochloric acid or carbonic acid in the presence of a solvent in a salt formation reactor 1. The salt of the amine compound obtained in the salt formation reactor 1 is supplied to a phosgene reactor 110 of a phosgene reaction unit 100 through a salt supply line 10 of the amine compound. The gas phase discharged from the salt formation reactor 1 is transferred to a surge drum 251 of a gas compression unit 250 through a gas phase discharge line 9.
The supply ratio of the anhydrous hydrochloric acid or carbonic acid may be, for example, 2 to 10 moles, 2 to 6 moles, or 2 to 4 moles, based on 1 mole of the amine compound.
Preferably, the amine compound may be a fatty amine having an aliphatic group in its molecule. Specifically, the aliphatic amine may be a chained or cyclic aliphatic amine. More specifically, the aliphatic amine may be a bifunctional or higher chained or cyclic aliphatic amine containing at least two amino groups in its molecule.
For example, the amine compound may be at least one compound selected from the group consisting of hexamethylenediamine, 2,2-dimethylpentanediamine, 2,2,4-trimethylhexanediamine, butenediamine, 1,3-butadiene-1,4-diamine, 2,4,4-trimethylhexamethylenediamine, 1,6,11-undecatriamine, 1,3,6-hexamethylenetriamine, 1,8-diisocyanato-4-(isocyanatomethyl)octane, bis(aminoethyl)carbonate, bis(aminoethyl)ether, xylylenediamine, α,α,α′,α′-tetramethylxylylenediamine, bis(aminoethyl)phthalate, bis(aminomethyl)cyclohexane, dicyclohexylmethanediamine, cyclohexanediamine, methylcyclohexanediamine, dicyclohexyldimethylmethanediamine, 2,2-dimethyldicyclohexylmethanediamine, 2,5-bis(aminomethyl)bicyclo-[2,2,1]-heptane, 2,6-bis(aminomethyl)bicyclo-[2,2,1]-heptane, 3,8-bis(aminomethyl)tricyclodecane, 3,9-bis(aminomethyl)tricyclodecane, 4,8-bis(aminomethyl)tricyclodecane, 4,9-bis(aminomethyl)tricyclodecane, bis(aminomethyl)norbornene, and xylylenediamine.
Further, the amine compound may be at least one sulfur-containing aliphatic amine selected from the group consisting of bis(aminomethyl)sulfide, bis(aminoethyl)sulfide, bis(aminopropyl)sulfide, bis(aminohexyl)sulfide, bis(aminomethyl)sulfone, bis(aminomethyl)disulfide, bis(aminoethyl)disulfide, bis(aminopropyl)disulfide, bis(aminomethylthio)methane, bis(aminoethylthio)methane, bis(aminoethylthio)ethane, bis(aminomethylthio)ethane, and 1,5-diamino-2-aminomethyl-3-thiapentane.
Among the above amine compounds, xylylenediamine (XDA) can exhibit superior effects when applied to the method for preparing an isocyanate compound according to one embodiment of the invention. Preferably, the amine compound may be at least one compound selected from the group consisting of m-xylylenediamine, p-xylylenediamine and o-xylylenediamine.
According to an embodiment of the invention, the phosgene reaction step is progressed in a gas-liquid-solid three-phase reaction in which a salt of solid-phase amine compound and gas phase phosgene are reacted in the presence of a solvent. Accordingly, rapid reactions can be effectively suppressed, and side reactions and formation of by-products can be minimized.
When the salt of amine compound and phosgene are reacted in the presence of a solvent, phosgene may be charged at a time, or may be charged dividedly. For example, a small amount of phosgene can be primarily charged at a relatively low temperature, and reacted with the salt of amine compound to produce the intermediate. Subsequently, the remaining amount of phosgene can be secondarily charged at a relatively high temperature, and reacted with the intermediate to obtain a reaction solution containing an isocyanate compound. As an example, xylylene diamine and a small amount of phosgene are reacted to produce an intermediate in the form of a carbamoyl salt, to which the remaining amount of phosgene is then charged, and the intermediate in the form of a carbamoyl salt can be reacted with phosgene to form an aliphatic isocyanate such as xylylene diisocyanate.
Through such phosgene reaction steps, a time during which the final product isocyanate compound is exposed to high temperature can be minimized. Furthermore, the intermediate is formed at a relatively low temperature, thereby reducing a time during which a high temperature should be maintained in the whole reaction process. In addition, the amount of heat charged to the whole process can be reduced. Further, the high-temperature reaction time of phosgene can be relatively shortened, and the risk of explosive vaporization of phosgene can also be reduced.
The phosgene reaction step is progressed in the presence of a solvent containing at least one of an aromatic hydrocarbon-based solvent and an ester-based solvent. The solvent may be selected in consideration of the temperature at which the reaction step is progressed.
The aromatic hydrocarbon-based solvent may be a halogenated aromatic hydrocarbon-based solvent such as monochlorobenzene, 1,2-dichlorobenzene and 1,2,4-trichlorobenzene.
The ester-based solvent may be fatty acid esters such as amyl formate, n-butyl acetate, isobutyl acetate, n-amyl acetate, isoamyl acetate, methylisoamyl acetate, methoxybutyl acetate, sec-hexyl acetate, 2-ethylbutyl acetate, 2-ethylhexyl acetate, cyclohexyl acetate, methylcyclohexyl acetate, benzyl acetate, ethyl propionate, n-butyl propionate, isoamyl propionate, ethyl acetate, butyl stearate, butyl lactate, and amyl lactate; or aromatic carboxylic acid esters such as methyl salicylate, dimethyl phthalate and methyl benzoate.
According to one embodiment of the invention, the salt of amine compound in the phosgene reaction step may be contained in the solvent at a concentration of 20% by volume or less, for example, 1 to 20% by volume, or 5 to 20% by volume. When the concentration of the salt of amine compound contained in the solvent exceeds 20% by volume, a large amount of salt is likely to precipitate in the phosgene reaction step.
The phosgene reaction step may be progressed at a temperature of 165° C. or less, preferably 80° C. to 165° C.
According to one embodiment of the invention, when phosgene is dividedly charged in the phosgene reaction step, it can be charged in an amount of 10 to 30% by weight, or 12 to 30% by weight, or 15 to 28% by weight based on the entire amount of phosgene charged at a temperature of 80° C. to 100° C. or 85° C. to 95° C. Under such reaction conditions, rapid reactions are suppressed and an intermediate in the form of a carbamoyl-based salt can be selectively and effectively formed. Subsequently, while charging the remaining amount of phosgene at a temperature of 110° C. to 165° C. or 120° C. to 150° C., the intermediate and the phosgene can be reacted to obtain a reaction product containing an isocyanate compound.
The isocyanate compound may vary depending on the type of the amine compound used in the phosgene reaction step. For example, the isocyanate compound may be at least one compound selected from the group consisting of n-pentyl isocyanate, 6-methyl-2-heptane isocyanate, cyclopentyl isocyanate, hexamethylene diisocyanate(HDI), isophorone diisocyanate(IPDI), diisocyanatomethylcyclohexane(H6TDI), xylylene diisocyanate(XDI), diisocyanatocyclohexane(t-CHDI) and di(isocyanatocyclohexyl)methane(H12MDI).
In particular, the method for preparing an isocyanate compound according to an embodiment of the invention may be further useful for the preparation of xylylene diisocyanate (XDI). XDI includes 1,2-XDI (o-XDI), 1,3-XDI (m-XDI), and 1,4-XDI (p-XDI) as structural isomers.
The phosgene reaction step can be progressed either batchwise or continuously. The phosgene reaction step can be progressed in a phosgene reaction unit 100 that includes a reactor 110 having a rotating shaft; an amine compound salt supply line 10 and a phosgene supply line 20 that supply reactants to the inside of the reactor; a heat source that supplies a heat quantity to the reactor; a reaction product transfer line 102 that transfers the reaction product obtained in the reactor to a subsequent step; and a gas phase discharge line 109 that transfers the gas phase obtained from the reactor to the surge drum 251 of the gas compression unit 250.
(Degassing Step)
Then, a degassing step of removing the gas phase from the reaction product is progressed.
In the degassing step, a gas phase such as surplus phosgene or byproduct hydrogen chloride is removed from the reaction product by a known degassing unit 200.
A method of removing the gas phase from the reaction product may include a method of supplying and aerating gas, or a method of separating the gas phase from the reaction product using a flash tank or a distillation column.
In particular, according to an embodiment of the invention, in order to minimize the formation of by-products in the degassing step, the degassing step is preferably progressed at a temperature of 145° C. to 165° C. and a pressure of 100 torr to 600 torr.
In one example, the degassing step may be progressed in a distillation column, wherein setting the temperature at the bottom of the distillation column to 145° C. to 165° C. and operating the distillation column under a column top pressure of 100 torr to 600 torr may be advantageous to minimize the formation of by-products. Here, the temperature at the bottom of the distillation column may mean the temperature of a reboiler connected to the bottom of the distillation column. And, the pressure at the top of the distillation column may mean the pressure of a condenser connected to the top of the distillation column.
Preferably, the temperature at which the degassing step is progressed may be 145° C. to 165° C., or 150° C. to 165° C., or 150° C. to 160° C., or 155° C. to 160° C. And, preferably, the pressure at which the degassing step is progressed may be 100 torr to 600 torr, or 200 torr to 500 torr, or 300 torr to 450 torr, or 350 torr to 450 torr.
When the temperature and pressure at which the degassing step is progressed do not satisfy the above ranges, the formation of by-products in the degassing step can increase, and the removal efficiency of a gas phase can decrease, whereby the concentration of the isocyanate compound in the reaction product obtained from the degassing step can decrease.
As an example, the degassing step can be progressed in a degassing unit 200 including a distillation column 220 configured so as to be able to remove a gas phase from the reaction product supplied via the reaction product transfer line 102 of the reaction unit 100; a gas phase discharge line 209 that discharges a gas phase to the top of the distillation column; and a reaction product transfer line 203 that discharges the reaction product from which the gas phase has been removed to the bottom of the distillation column and transfers it to a subsequent step.
(Gas Compression Step)
Then, a gas compression step is progressed in which the gas phase obtained in the degassing step is compressed to obtain a gas phase condensate.
In the gas compression step, the gas phase obtained in the degassing step is compressed under a gas compression unit 250 to obtain the gas phase condensate.
Preferably, in the gas compression step, the gas phase obtained in the phosgene reaction step together with the gas phase obtained in the degassing step is compressed under a gas compression unit 250 to obtain the gas phase condensate.
More preferably, in the gas compression step, the gas phase obtained in the salt formation reaction step, the phosgene reaction step and the degassing step is compressed under a gas compression unit 250 to obtain the gas phase condensate.
Preferably, in order to secure the compression efficiency of the gas phase and the pressure of the condensate, the gas compression step may be progressed under a gas compression unit 250 including three or more gas compressors. Preferably, the gas compression step may be progressed under a gas compression unit 250 including three or more stages of centrifugal compressors. Preferably, the gas compression unit 250 includes three or more sub-units including a surge drum 251, a gas compressor 254, and a condenser 257.
As an example,
Among them, the gas phase is supplied from the gas phase discharge line 209 of the degassing unit 200 to the surge drum 251 of the first sub unit. Optionally, the gas phase transferred from the gas phase discharge line 9 of the salt formation reactor 1 and the gas phase discharge line 109 of the phosgene reaction unit 100 may be further supplied to the surge drum 251.
The lower part of the surge drum 251 separates liquid droplets through a droplet discharge line 252, thereby preventing the liquid phase from flowing into the gas compression unit 250. The gas phase is discharged to the upper part of the surge drum 251, and the gas phase is supplied to the gas compressor 254 through a gas phase transfer line 253. The gas phase is compressed in a gas compressor 254. The compressed gas obtained from the gas compressor 254 is supplied to the condenser 257 through a compressed gas transfer line 256.
In order to prevent a surge phenomenon when the operation of the gas compressor 254 is stopped due to a power failure or the like, a portion of the gas phase that is not compressed in the gas compressor 254 is supplied to the surge drum 251 through the gas recirculation line 255. The compressed gas is supplied to the condenser 257 to reduce its temperature, and is supplied to the surge drum 261 of the second sub unit through a transfer line 259.
In the second subunit and the third subunit, compression of gas is conducted with the same flow as in each device corresponding to the first subunit.
Finally, the condensate obtained in the condenser 277 of the third unit is transferred to a buffer drum 280 through a condensate transfer line 279. The condensate collected in the buffer drum 280 is supplied as a feed to the distillation tower 291 of the distillation unit 290.
In the gas compression unit 250, the surge drums 251, 261 and 271 are devices for preventing surges during the gas compression process. Although not shown in
In the gas compression unit 250, the gas compressors 254, 264 and 274 are devices for compressing the gas phase to form compressed gas. Preferably, in the gas compression step, the gas phase is preferably compressed to a pressure of 16 bar or more in order to ensure the compression efficiency of the gas phase and the sufficient pressure of the condensate.
For example, it is preferable that the gas phase flowing into the first subunit exhibits a pressure of 16 bar or more in the last subunit after passing through each subunit.
More preferably, in the gas compression step, the gas phase can be compressed to a pressure of 16 bar to 19 bar, or 16.5 bar to 18.5 bar, or 16.5 bar to 18 bar.
(Distillation Step)
Then, a distillation step is progressed in which the condensate obtained in the compression step is distilled to separate phosgene from the condensate.
In the distillation step, phosgene is separated and recovered from the condensate by a distillation unit 290 including a distillation column 291.
According to one embodiment of the invention, in order to secure the distillation efficiency of the condensate and the energy efficiency of the entire process, the distillation step is preferably progressed under a distillation column 291 whose column top temperature is −15° C. or more. Preferably, the temperature at the top of the distillation column 291 may be −15° C. to 0° C., −12° C. to −3° C., or −10° C. to −5° C.
According to one embodiment of the invention, the temperature at the top of the distillation column 291 can be determined depending on the pressure of the condensate supplied to the distillation step in the gas compression step. For example, when the final pressure of the condensate supplied from the gas compression step to the distillation step (i.e., the pressure of the condensate discharged from the last subunit of the gas compression unit 250) is 16 bar or more, the distillation column 291 can be operated at a column top temperature of −15° C. or more. The lower the column temperature must be set during operation of the distillation column 291, the more energy is consumed, which can reduce energy efficiency and process efficiency.
In the distillation step, the condensate collected in the buffer drum 280 is supplied as a feed to the distillation column 291. By the distillation in the distillation column 291, the phosgene-containing fraction separated from the condensate is discharged to the lower part of the distillation column 291 through a bottom stream line 292.
The phosgene-containing fraction is supplied to a reboiler 294. In the reboiler 294, the low boiling fraction is re-supplied to the bottom of the distillation column 291, and the remaining fraction, i.e., phosgene, is recovered through the phosgene discharge line 296. The recovered phosgene is used as a reactant in the reaction step. That is, phosgene recovered through the phosgene discharge line 296 in the distillation step is supplied to the reactor 110 through the phosgene supply line 20 of the reaction unit 100.
In the distillation step, the gas phase (e.g., hydrochloric acid gas or carbon dioxide gas) separated from the condensate is discharged to the top of the distillation column through a column top stream line 293. The discharged gas phase is supplied to the condenser 295. A part of the gas phase condensed in the condenser 295 is re-supplied to the top of the distillation column 291, and the rest is recovered through the gas phase discharge line 297. The recovered gas phase is used as a reactant to form a salt of the amine compound.
Meanwhile, according to another embodiment of the invention, the method for preparing an isocyanate compound may further comprise a desolvation step of removing a solvent from the reaction product from which the gas phase obtained in the degassing step has been removed, a low boiling material-removing step of removing low boiling materials (i.e., lights) from the reaction product from which the solvent has been removed, and a high boiling material-removing step of removing high boiling materials (i.e., heavies) from the reaction product from which the low boiling materials have been removed.
(Desolvation Step)
Then, a desolvation step may be progressed in which a solvent is removed from the reaction product from which the gas phase has been removed.
In the desolvation step, the solvent is distilled off from the reaction product from which the gas phase has been removed by a known desolvation unit 300.
According to one embodiment of the invention, in order to minimize thermal denaturation of the reaction product and formation of by-products in the desolvation step, the desolvation step is preferably progressed at a temperature of 100° C. to 165° C. and a pressure of 30 torr or less.
In one example, the desolvation step can be progressed in a distillation column, wherein setting the temperature at the bottom of the distillation column to 100° C. to 165° C. and operating the distillation column under a column top pressure of 30 torr or less can be advantageous to minimize the thermal degradation and the formation of by-products. Here, the temperature at the bottom of the distillation column may mean the temperature of a reboiler connected to the bottom of the distillation column. And, the pressure at the top of the distillation column may mean the pressure of a condenser connected to the top of the distillation column.
Preferably, the temperature at which the desolvation step is progressed may be 100° C. to 165° C., or 115° C. to 165° C., or 115° C. to 160° C., or 130° C. to 160° C. And, preferably, the pressure at which the desolvation step is progressed may be 5 torr to 30 torr, or 5 torr to 25 torr, or 10 torr to 20 torr, or 10 torr to 15 torr.
When the temperature and pressure at which the desolvation step is progressed do not satisfy the above ranges, the thermal denaturation and the formation of by-products in the desolvation step may increase, and the solvent removal efficiency may decrease, whereby the concentration of the isocyanate compound in the reaction product obtained from the desolvation step may decrease.
In one example, the desolvation step can be progressed in a desolvation unit 300 that includes a distillation column 330 configured so as to be able to remove a solvent from the reaction product supplied via the reaction product transfer line 203 of the degassing unit 200; a solvent discharge line 309 that discharges a solvent to the top of the distillation column; and a reaction product transfer line 304 that discharges the reaction product from which the solvent has been removed to the bottom of the distillation column, and transfers it to a subsequent step.
In order to minimize the high temperature residence time of the reaction product in the desolvation step, a distillation column 440 equipped with apparatuses such as a kettle type reboiler, a thin-film evaporator, a force circulated reboiler, and a jacketed vessel type reboiler can be utilized.
(Low Boiling Material-Removing Step)
Then, a low boiling material-removing step may be progressed in which low boiling materials (i.e., lights) are removed from the reaction product from which the solvent obtained in the desolvation step has been removed.
In the low boiling material-removing step, the low boiling materials (lights) are removed by a known low boiling material-removing unit 400 from the reaction product from which the solvent has been removed.
The low boiling material means a material having a boiling point lower than that of the isocyanate compound, which is the main product in the reaction step. Examples of the low boiling materials include materials produced by side reactions in the process of obtaining the main product. As an example, in the process of preparing XDI as the isocyanate compound, the low boiling material may include monoisocyanate such as (chloromethyl)benzyl isocyanate (CBI) and ethylphenyl isocyanate (EBI).
According to one embodiment of the invention, in order to minimize the thermal denaturation of reaction products and the formation of by-products in the low boiling material-removing step, the low boiling material-removing step is preferably progressed under the conditions where the temperature at the bottom of the distillation column 440 is set to 150° C. to 165° C. and the pressure at the top of the distillation column is set to 5 torr or less. Here, the temperature at the bottom of the distillation column may mean the temperature of a reboiler connected to the bottom of the distillation column.
Preferably, the temperature at which the low boiling material-removing step is progressed may be 150° C. to 165° C., or 155° C. to 165° C., or 155° C. to 162° C., or 160° C. to 162° C. And, preferably, the upper pressure at which the low boiling material-removing step is progressed may be 1 torr to 5 torr, or 2 torr to 5 torr, or 2 torr to 4 torr.
If the temperature and pressure at which the low boiling material-removing step is progressed do not satisfy the above ranges, the thermal denaturation and the formation of by-products in the low boiling material-removing step may increase, and the removal efficiency of low boiling materials may decrease, whereby the concentration of isocyanate compounds in the reaction product obtained from the low boiling material-removing step can be reduced.
In one example, the low boiling material-removing step can be progressed in a low boiling material-removing unit 400 that includes a distillation column 440 configured so as to be able to remove low boiling materials from the reaction product supplied through the reaction product transfer line 304 of the desolvation unit 300; a low boiling material discharge line 409 that discharges low boiling materials to the top of the distillation column; and a reaction product transfer line 405 that discharges the reaction product from which the low boiling materials have been removed to the bottom of the distillation column, and transfers it to a subsequent step.
In order to minimize the high temperature residence time of the reaction product in the low boiling material-removing step, a distillation column 440 equipped with apparatuses such as a kettle type reboiler, a thin-film evaporator, a force circulated reboiler, and a jacketed vessel type reboiler can be utilized.
(High Boiling Material-Removing Step)
Then, a high boiling material-removing step may be progressed in which high boiling materials (i.e., heavies) are removed from the reaction product from which the low boiling materials obtained in the low boiling material-removing step have been removed.
In the high boiling material-removing step, high boiling materials (i.e., heavies) are removed by a known high boiling material-removing unit 500 from the reaction product from which the low boiling materials have been removed.
The high boiling material means a material having a boiling point higher than that of the isocyanate compound, which is the main product in the reaction step. Examples of the high boiling materials include high-molecular-weight by-products such as oligomers or polymers including dimers, trimers or higher multimers of isocyanate compounds formed in the step of obtaining the main product.
According to one embodiment of the invention, in order to minimize the thermal denaturation of the reaction product and the formation of by-products in the high boiling material-removing step, the high boiling material-removing step may preferably be progressed at a temperature of 145° C. to 165° C. and a pressure of 1 torr or less.
In one example, the high boiling material-removing step may be progressed under a thin-film evaporator, wherein setting the temperature at the bottom of the distillation column to 145° C. to 165° C. and operating the distillation column under a column top pressure of 1 torr or less can be advantageous to minimize the thermal degradation and the formation of by-products.
Preferably, the temperature at which the high boiling material-removing step is progressed may be 145° C. to 165° C., or 150° C. to 165° C., or 150° C. to 160° C., or 155° C. to 160° C. And, preferably, the pressure at which the high boiling material-removing step is progressed may be 0.1 torr to 1 torr, or 0.5 torr to 1 torr.
If the temperature and pressure at which the high boiling material-removing step is progressed do not satisfy the above ranges, the thermal denaturation and the formation of by-products in the high boiling material-removing step may increase, and the removal efficiency of high boiling materials may decrease, whereby the concentration of the isocyanate compound obtained from the high boiling material-removing step may decrease.
In one example, the high boiling material-removing step may be progressed in a high boiling material-removing unit 500 that includes a thin-film evaporator 550 configured so as to be able to remove high boiling materials from the reaction product supplied through the reaction product transfer line 405 of the low boiling material-removing unit 400; an isocyanate compound discharge line 509 that discharges an isocyanate compound to a condensing section of the thin-film evaporator; and a high boiling material discharge line 506 that discharges the high boiling material to the bottom of the thin-film evaporator.
According to the present invention, provided is a method for preparing an isocyanate compound that can recover and reuse materials used in the reaction during the preparation of an isocyanate compound using phosgene, and can minimize thermal denaturation of a reaction product and formation of by-products.
Hereinafter, the actions and effects of the invention will be explained in more detail through specific examples of the invention. However, these examples are presented only as the illustrations of the invention, and the scope of the right of the invention is not determined thereby.
1,3-XDI (m-XDI) was prepared by the following process using the apparatus shown in
(Phosgene Reaction Step)
Under normal temperature and pressure conditions, 500 kg of hydrochloric acid and 560 kg of m-xylylenediamine (m-XDA) were reacted in 6500 kg of 1,2-dichlorobenzene (o-DCB) solvent for 4 hours to form 870 kg of the hydrochloride salt of m-xylylenediamine. At this time, unreacted hydrochloric acid gas discharged through the gas phase discharge line 9 was transferred to a surge drum 251 of a gas compression unit 250.
870 kg of the hydrochloride salt of m-xylylenediamine was charged into a reactor 110 through a supply line 10, and the temperature of the reactor was raised to 125° C. During the progress of the reaction, a total of 1359 kg of phosgene was put into the reactor through the supply line 20, and stirred. A dry ice-acetone condenser was used from the time of charging phosgene to the time of completion of the reaction to prevent phosgene from leaking to the outside. The reaction was allowed to progress for 1.5 hours at a temperature of 90° C.
After that, the internal temperature of the reactor was heated to 125° C., and 6000 kg of phosgene was further charged. The temperature of the reactor was maintained at 125° C., and further stirred for 4.5 hours until the reaction solution became clear. Heating was stopped after the reaction solution became clear. The reaction product obtained by the above method was transferred to the degassing unit 200 through a transfer line 102. At this time, unreacted phosgene and hydrochloric acid gas discharged through the gas phase discharge line 109 were transferred to a surge drum 251 of a gas compression unit 250.
(Degassing Step)
The distillation column 220 of the degassing unit 200 was configured so as to be able to remove the gas phase from the reaction product supplied through the transfer line 102.
Specifically, the distillation column 220 used was a packing tower packed with Mellapak, which is a type of structural packing, and had a height of about 6 m.
The temperature at the bottom of the distillation column 220 was set to 155° C., and the distillation column 220 was operated under a column top pressure of 400 torr.
About 150 kg/hr of the reflux stream was re-charged to a distillation column 220, which corresponds to a reflux ratio of about 3.2 relative to the column top outflow amount.
The gas phase containing phosgene was discharged through a gas phase discharge line 209 connected to the top of the distillation column 220. The gas phase discharged via the gas phase discharge line 209 was transferred to a surge drum 251 of the gas compression unit 250. The reaction product from which the gas phase has been removed was transferred to the desolvation unit 300 through the transfer line 203 connected to the bottom of the distillation column 220.
(Gas Compression Step)
The gas phase supplied to the surge drum 251 of the first subunit in the gas compression unit 250 was supplied to a gas compressor 254 through a transfer line 253. In the gas compressor 254 the gas phase was compressed under a pressure of 2.7 bar. The compressed gas obtained from the gas compressor 254 was supplied to a condenser 257 through a transfer line 256. The temperature of the compressed gas supplied to the condenser 257 was lowered to 15° C., and the compressed gas was supplied to the surge drum 261 of the second subunit through a transfer line 259.
The compressed gas supplied to the surge drum 261 of the second subunit was supplied to the gas compressor 264 through the transfer line 263. In the gas compressor 264, the compressed gas was further compressed under a pressure of 7.6 bar. The compressed gas obtained from the gas compressor 264 was supplied to the condenser 267 through a transfer line 266. The temperature of the compressed gas supplied to the condenser 267 was lowered to 41° C., and the compressed gas was supplied to a surge drum 271 of the third subunit through a transfer line 269.
The compressed gas supplied to the surge drum 271 of the third subunit was supplied to the gas compressor 274 through the transfer line 273. In the gas compressor 274, the compressed gas was further compressed under a pressure of 16.86 bar (12644 torr). The compressed gas obtained from the gas compressor 274 was supplied to the condenser 277 through a transfer line 276. The temperature of the condensate supplied to the condenser 277 was lowered to −5° C. to form a condensate. The condensate was transferred to a buffer drum 280 through a transfer line 279.
(Distillation Step)
The condensate collected in the buffer drum 280 was supplied as a feed to the distillation tower 291 of the distillation unit 290. The distillation column 291 was configured so as to be able to separate phosgene from the condensate.
Specifically, the distillation column 291 is an about 8 m column composed of 12 bubble cap trays. About 710 kg/hr of the reflux stream was re-charged to the distillation column 291, which corresponds to a reflux ratio of about 3 relative to the column top outflow amount.
As the condensate from the gas compression step is supplied to the distillation column 291 at a pressure of 16.86 bar, the condenser 295 connected to the top of the distillation column 291 was operated at a temperature of −15° C.
The phosgene-containing fraction separated from the condensate was discharged to the bottom of the distillation column 291 through a bottom stream line 292. The phosgene-containing fraction was supplied to the reboiler 294. The low boiling fraction in the reboiler 294 was re-supplied to the bottom of the distillation column 291, and the remaining fraction, i.e., phosgene, was recovered through a phosgene discharge line 296. The recovered phosgene was supplied to a reactor 110 through the phosgene supply line 20 of the reaction unit 100.
The fraction-containing hydrochloric acid gas separated from the condensate was discharged to the top of the distillation column 291 through a column top stream line 293. The discharged hydrochloric acid gas-containing fraction was supplied to a condenser 295. A part of the fraction condensed in the condenser 295 was re-supplied to the top of the distillation column 291, and the remaining hydrochloric acid gas was recovered through a gas phase discharge line 297. The recovered hydrochloric acid gas was supplied to the reaction step as a reactant for forming a salt of amine compound.
(Desolvation Step)
The distillation column 330 of the desolvation unit 300 was configured so as to be able to remove the solvent from the reaction product supplied through the transfer line 203.
Specifically, the distillation column 330 used was a packing tower packed with Mellapak, which is a type of structural packing, and had a height of about 7 m.
The temperature at the bottom of the distillation column 330 was set to 160° C., and the distillation column 330 was operated under a column top pressure of 15 torr.
About 600 kg/hr of the reflux stream was re-charged to the distillation column 330, which corresponds to a reflux ratio of about 0.5 relative to the column top outflow amount.
A solvent including 1,2-dichlorobenzene (o-DCB) was discharged through a solvent discharge line 309 connected to the top of the distillation column 330. The reaction product from which the solvent has been removed was transferred to the degassing unit 400 through the transfer line 304 connected to the bottom of the distillation column 330.
(Low Boiling Material-Removing Step)
The distillation column 440 of the high boiling material-removing unit 400 was configured so as to be able to remove low boiling materials from the reaction product supplied through the transfer line 304.
Specifically, the distillation column 440 used was a packing tower packed with Mellapak, which is a type of structural packing, and had a height of about 13 m.
The temperature at the bottom of the distillation column 440 was set to 160° C., and the distillation column 440 was operated at column top pressure of 5 torr.
About 40 kg/hr of the reflux stream was re-charged to the distillation column 440, which corresponds to a reflux ratio of about 2.0 relative to the column top outflow amount.
Low boiling materials including (chloromethyl)benzyl isocyanate (CBI) were discharged through the low boiling material discharge line 409 connected to the top of the distillation column 440. The reaction product from which the low boiling materials were removed was transferred to the high boiling material-removing unit 500 through a transfer line 405 connected to the bottom of the distillation column 440.
(High Boiling Material-Removing Step)
The thin-film evaporator 550 of the high boiling material-removing unit 500 was configured so as to be able to remove high boiling materials from the reaction product supplied through the transfer line 405.
Specifically, the thin-film evaporator 550 used was an evaporator in the form of a short path evaporator having a condenser installed therein.
The bottom temperature of the thin-film evaporator 550 was set to 160° C., and the thin-film evaporator 550 was operated under an evaporator bottom pressure of 0.5 torr.
About 13 kg/hr of high boiling condensate was separated from the bottom of the thin-film evaporator.
Isocyanate compounds including 1,3-XDI (m-XDI) were discharged through the discharge line 509 connected to the top of the thin-film evaporator 550. The high boiling material separated from the reaction product was discharged through a discharge line 506 connected to the bottom of the thin-film evaporator 550.
An isocyanate compound including 1,3-XDI (m-XDI) was obtained in the same manner as in Example 1, except that in the gas compression step, compression in the gas compressor 274 of the last subunit was conducted under a pressure of 20 bar.
As the condensate from the gas compression step was supplied to the distillation column 291 at a pressure of 20 bar, the condenser 295 connected to the top of the distillation column 291 was operated at a temperature of −9.2° C.
An isocyanate compound including 1,3-XDI (m-XDI) was prepared in the same manner as in Example 1, except that in the gas compression step, compression in the gas compressor 274 of the last subunit was conducted under a pressure of 10 bar.
As the condensate from the gas compression step was supplied to the distillation column 291 at a pressure of 10 bar, the condenser 295 connected to the top of the distillation column 291 was operated at a temperature of −32° C.
Part of the stream of the gas phase discharge line 297 and the phosgene discharge line 296 of the distillation unit 290 in Examples and Reference Example was recovered, and subjected to gel permeation chromatography analysis. The contents of the main components identified through the above analysis are shown in Tables 1 to 3 below.
In addition, the energy per unit time (kcal/hr) charged to the gas compression step and the distillation step of Examples and Comparative Examples was measured, and shown in Tables 1 to 3 below.
Referring to Tables 1 to 3, it was confirmed that the method for preparing an isocyanate compound according to Examples can efficiently recover and reuse phosgene and hydrochloric acid used in the reaction step, with a relatively low energy consumption.
Even in Reference Example, phosgene and hydrochloric acid could be recovered from the distillation unit through the gas compression step, but in the gas compression step, sufficient pressure of the compressed gas was not secured, and thus, a large amount of energy was consumed per unit time. In particular, in Reference Example, since a large amount of expensive refrigerant must be used to keep the temperature at the top of the column low during operation of the distillation column, the difference in economic effect compared to Examples was shown to be large.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10-2020-0187831 | Dec 2020 | KR | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/KR2021/020325 | 12/30/2021 | WO |
