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  • C07C39/15—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring polycyclic with no unsaturation outside the aromatic rings with all hydroxy groups on non-condensed rings, e.g. phenylphenol
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  • B01J2208/00796—Details of the reactor or of the particulate material
  • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
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  • B01J2219/00222—Control algorithm taking actions
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  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/06—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing polymers
  • B01J31/08—Ion-exchange resins
  • B01J31/10—Ion-exchange resins sulfonated

Definitions

• the present invention relates to a method for producing bisphenol A and a vertical fixed bed reactor, and more specifically, by eliminating the drift (channeling) of a reaction solution flowing through an ion exchange resin catalyst in the reactor.
• the present invention also relates to a method for producing bisphenol A and a vertical fixed bed reactor that can prevent local catalyst deterioration and stably produce bisphenol A for a long period of time.
• Bisphenol A is usually produced by reacting phenol and acetone in the presence of an acidic catalyst.
• an acidic catalyst a sulfonic acid type cation exchange resin is generally used from the viewpoint of high reaction rate and good selectivity.
• the reaction is usually carried out continuously by flowing a phenol raw material and an acetone raw material in a downward flow through a vertical fixed bed reactor packed with a sulfonic acid type cation exchange resin catalyst. After a certain period of reaction, the operation is stopped and the deteriorated catalyst is washed or replaced.
• Patent Document 1 Japanese Patent Application Laid-Open No. 2005-162742
• Patent Document 2 Japanese Patent Publication No. 49-48319
• Patent Document 3 JP-A-1-230538
• Patent Document 4 Japanese Patent Laid-Open No. 5-331088
• the present invention has been made in view of the above circumstances, and its purpose is to eliminate local catalyst degradation by eliminating the drift of the reaction liquid flowing through the ion exchange resin catalyst in the reactor.
• the present invention provides a method for producing bisphenol A and a vertical fixed bed reactor that can stably produce bisphenol A for a long period of time.
• the first aspect of the present invention is a reaction solution in which a phenol raw material and an acetone raw material are circulated through a solid fixed bed reactor packed with an ion exchange resin catalyst to obtain a bisphenol A-containing reaction solution.
• the outlet force of the ion-exchange resin catalyst layer formed in the reactor is also within the range of the catalyst layer height within 20%.
• the absolute value of the temperature difference ( ⁇ ) between the temperature of the liquid and the temperature of the reaction liquid at the outlet of the fixed bed reactor is 1.0 to 5.0 ° C
• at least one of the ion exchange resin catalysts resides in a method for producing bisphenol A, which is characterized by flowing the part.
• the second gist of the present invention is a solid fixed-bed reactor filled with an ion-exchange resin catalyst, wherein the exit force of the ion-exchange resin catalyst layer is within the range of 20% or less of the catalyst layer height.
• This is a vertical fixed bed reactor characterized in that the temperature of the reaction solution at at least two points at these positions is measurable.
• the drift of the reaction solution flowing through the ion exchange resin catalyst in the reactor is prevented, local catalyst deterioration is prevented, and bisphenol A is used for a long time. It can be manufactured stably.
• FIG. 1 is an explanatory diagram of a vertical fixed bed reactor used in Example 1 of the present invention.
• the method for producing bisphenol A of the present invention is a reaction step in which a phenol raw material and an acetone raw material are circulated through a vertical fixed bed reactor filled with an ion exchange resin catalyst to obtain a reaction liquid containing bisphenol A. Is included.
• the reaction step in the present invention uses a vertical fixed bed reactor filled with an ion exchange resin as a catalyst.
• the phenol feed and acetone feed fed to the vertical fixed bed reactor are reacted stoichiometrically in excess of phenol.
• the molar ratio of phenol to acetone (phenol Z acetone) is usually 3 to 30, preferably 5 to 20.
• the liquid space velocity of the raw material mixture supplied to the reactor is usually 0.2 to 50 Zh.
• the reaction temperature is usually 30 to 120 ° C, preferably 55 to 100 ° C.
• the reaction pressure is usually normal pressure to 600 kPa.
• the above phenol raw material is a raw material mainly composed of phenol, and the phenol content is usually 50% by weight or more, preferably 70% by weight or more, and more preferably 80% by weight or more. Pure phenol can be used, but other compounds may include bisphenol A, its 2,4 isomers, chroman, trisphenol, isopropylphenol and cyclic dimers. ,.
• the mother liquor separated in the recovery process for collecting bisphenol A, the reaction liquid treated in the impurity treatment process, etc. can be used as they are, or these mixed liquids can be recycled.
• the acetone raw material is a raw material mainly composed of acetone, and the acetone-containing ratio is usually 50% by weight or more, preferably 70% by weight or more, more preferably 90% by weight or more, particularly Preferably it is 95 weight% or more. Pure acetone can be used, but it may contain impurities such as water. Acetone separated and recovered in the acetone circulation step can be used as it is or by recycling a mixture with pure acetone.
• a strong acid cation exchange resin such as a sulfonic acid type is preferably used.
• the catalyst is usually used with a cocatalyst such as a sulfur-containing compound.
• a method of supplying a fluorine-containing compound such as hydrogen sulfide and alkylthiol together with a phenol raw material and a acetone raw material (method 1), and a method of using an ion-exchanged resin in which a fluorine-containing compound is bound in advance as a catalyst (method) There is 2).
• Method 1 as the alkyl thiol, methane thiol, ethane thiol, open pan thiol or the like is used.
• Method 2 a resin obtained by modifying a strongly acidic cation exchange resin partially with a thioamine compound is preferably used.
• thioamine-containing compounds examples include 2- (4 pyridyl) ethanethiol, 2 mercaptoethylamine, 3-mercaptopropylamine, N, N dimethyl-3-mercaptopropylamine, N, N-di-n-butyl-4
• Common promoters used for the synthesis of bisphenol A such as mercaptobutyramine and 2,2 dimethylthiazolidine, can be used.
• the vertical fixed bed reactor used in the method for producing bisphenol A of the present invention has an outlet (in the case of a downward flow, in the case of a downward flow). It is characterized in that the temperature of the reaction solution at at least two positions in any position within the range of the catalyst layer height within 20% from the most downstream part) can be measured.
• the outlet of the catalyst layer means a place where the reaction solution that has passed through the catalyst layer comes out of the catalyst layer.
• it means a contact surface between the catalyst support member (reference numeral 3 in FIG. 1) and the catalyst layer (reference numeral 4 in FIG. 1).
• An example of the temperature measuring device is a thermocouple thermometer.
• the catalyst layer center part and the catalyst layer support member downstream part are two points, more preferably the catalyst layer center part, the peripheral part, and the catalyst layer support.
• a piping part etc. of the member downstream are mentioned.
• measurement can be performed at a plurality of locations in the height direction of the catalyst layer, which is determined only by the temperature in the horizontal direction of the catalyst layer. This is because it can be known that the temperature change in the flow direction of the reaction liquid does not increase monotonously. However, it is preferable that no drift occurs in the catalyst layer by installing a thermometer.
• the vertical fixed bed reactor of the present invention is preferably an adiabatic reactor because it measures the temperature change in the catalyst layer as described above.
• the temperature can be measured as described above, and a phenol raw material and an acetone raw material are circulated through a fixed type fixed bed reactor filled with an ion exchange resin catalyst to obtain a bisphenol A-containing reaction solution.
• the outlet force of the ion exchange resin catalyst layer is also within 20% of the catalyst layer height.
• a drift flow is formed in the catalyst layer, and the load on the catalyst around the flow path with a large flow rate increases, resulting in a decrease in the reaction rate and the reaction liquid compared to other portions.
• the temperature becomes lower. Further, in the portion where the flow rate is small, the catalyst load is small, so that the reaction rate becomes high and the temperature of the reaction solution becomes high.
• the outlet force of the ion exchange resin catalyst layer is also the temperature of the reaction solution at any position where the catalyst layer height is within a range of 20% or less, and the outlet of the rigid fixed bed reactor.
• the absolute value of the temperature difference ( ⁇ ) from the temperature of the reaction solution reaches 1.0 to 5.0 ° C, at least a part of the ion exchange resin catalyst is allowed to flow.
• the drift in the catalyst layer is canceled and the catalyst load can be returned to a stable state in the initial stage of the reaction before the catalyst deteriorates, and the life of the catalyst can be extended.
• the ion exchange resin catalyst it is possible to flow at least part of the ion exchange resin catalyst when the absolute value of the temperature difference ( ⁇ ) is less than 1.0 ° C, but under normal operating conditions it is 1.0 ° C or more. If this happens, it is possible to sufficiently prevent the catalyst from degrading, and to stop the reaction too often and to flow at least a part of the ion-exchange resin catalyst is necessary for stable operation and production.
• the surface area of efficiency is also not preferable. Even if the absolute value of the temperature difference ( ⁇ ) exceeds 5.0 ° C and at least a part of the ion exchange resin catalyst is flowed, the recovery effect of the caseon conversion rate can be seen temporarily. However, since the catalyst has already deteriorated, the production efficiency is significantly worse than the initial reaction state, which is difficult to recover sufficiently.
• the preferable range of absolute value of temperature difference ( ⁇ ) is 1.5 to 4.0.
• the method of flowing at least a part of the ion exchange resin catalyst is not particularly limited.
• a method of supplying a fluid in an upflow to a downflow vertical fixed bed reactor For example, a method of flowing the catalyst layer by a mechanical means such as a stirrer or using a device that applies vibration to the catalyst layer may be used.
• the back washing method is preferable because it does not require a new auxiliary device and can uniformly flow the entire catalyst layer.
• the fluid supplied to the fixed type fixed bed reactor in an upward flow is not particularly limited, and a fluid that can flow a catalyst such as water or phenol is preferably used.
• a fluid that can flow a catalyst such as water or phenol is preferably used.
• raw material phenol or pure phenol is used. Use.
• FIG. 1 shows a reactor and a flow diagram used in Example 1 described later.
• valves 81 and 82 are opened, valves 83 and 84 are closed, and pump 7 is used to feed phenol and gasoline feed to reactor 1 via lines 91 and 92.
• the reactor 1 has a catalyst layer 4 having a height of 'on the catalyst support member 3, and the reaction raw material is circulated in a downward flow, and the reaction liquid obtained via the line 93 and the valve 82 is passed through. To the process.
• valves 81 and 82 are closed, valves 83 and 84 are opened, and only the phenol raw material is supplied to reactor 1 in an upward flow through lines 91 and 94 using pump 7.
• the phenol raw material supplied in the upward flow cleans the catalyst layer 4 and is discharged through the line 95 and the valve 84. At this time, the flow of the catalyst layer occurs, and the uneven flow path in the catalyst layer formed at the time of the reaction is eliminated, so that the catalyst is returned to a uniformly packed state.
• the flow rate of the reaction solution is usually set to a value equal to or higher than the minimum fluidization speed and equal to or lower than 120%, and the catalyst layer is preferably back-washed until the flow rate is 0.5 times or more of the catalyst amount. . At that time, it is preferable to set the speed so that the backwashed catalyst does not flow out of the reactor from the top of the reactor.
• the minimum fluidization speed can be obtained by calculating the specific gravity of the fluid or ion exchange resin, the particle size and weight force of the ion exchange resin, or by actually conducting experiments. After backwashing, switch the valve, start supplying the reactants and restart the reaction.
• each step performed subsequent to the reaction step includes a low-boiling component separation step for separating the reaction mixture obtained in the reaction step into a component containing bisphenol A and a low-boiling component containing unreacted acetone, Crystallization step of crystallizing bisphenol A as an adjunct with phenol from a component containing bisphenol A to obtain a slurry, and the slurry obtained in the crystallization step is adduct crystal of bisphenol A and phenol Recovery process for recovering adduct crystals of bisphenol A and phenol by separating it into a mother liquor, and separating the mother liquor into light and heavy components by distilling the separated mother liquor after alkali heat treatment and recombining the light components
• Examples include an impurity treatment step for reaction treatment and an acetone circulation step for separating and recovering unreacted acetone from the low boiling point component obtained in
• the vertical fixed bed reactor shown in Fig. 1 was used.
• the bottom radius of reactor 1 is 2.8 m, and 15% of the sulfonic acid groups are 2- (4-pyridyl) ethane so that the catalyst layer height is 3.25 m (catalyst amount: 80 m 3 ).
• a sulfonic acid type cation exchange resin catalyst modified with thiol was packed.
• Two thermocouple thermometers 5 were installed in the catalyst layer. As shown in Fig. 1, the installation location is the same position where the distance r from the outer periphery of the reactor is 250 cm in the horizontal direction of the catalyst layer, and 15 cm from the lowest surface of the catalyst layer in the height direction.
• the temperature at measurement point 1 is 72.9 ° C
• the temperature at measurement point 2 is 72.9 ° C
• the temperature at the reactor outlet (measurement point 0) is 69. 9 ° C. That is, the absolute value of the temperature difference between measurement point 1 and measurement point 0 was 3.0 ° C, and the absolute value of the temperature difference between measurement point 2 and measurement point 0 was 3.0 ° C.
• the acetone conversion was 87.5%.
• valves 81 and 82 are closed, valves 83 and 84 are opened, and only the phenol raw material is pumped up through line 91 and 94 using pump 7 at a temperature of 63.0 ° C and a flow rate of 15 tZh for 3 hours.
• it was supplied to the reactor 1 to flow the catalyst bed.
• the supply of the reaction raw material was restarted, and the reaction was started in a downward flow (down flow).
• the temperature at measurement point 1, measurement point 2 and reactor outlet (measurement point 0) at 10 hours after the start of the reaction was equal to 71.1 ° C.
• the temperature difference between measurement point 1 and measurement point 0 was 0.0 ° C
• the temperature difference between measurement point 2 and measurement point 0 was 0.0 ° C.
• the acetone conversion rate at this time was 94.5%. Thereafter, the operation was further continued, and the acetone conversion rate was 82.0% after 24 months from the start of the first reaction.
• Example 2 The same operation as in Example 1 was performed, except that the reaction was not stopped and the catalyst flow operation was not performed after 12 months from the start of the operation, and the operation was continued.
• the temperature at measuring point 1 is 71.9 ° C
• the temperature at measuring point 2 is 71.9 ° C
• the temperature was 65.9 ° C. That is, the temperature difference between measurement point 1 and measurement point 0 was 6.0 ° C, and the temperature difference between measurement point 2 and measurement point 0 was 6.0 ° C. At this point.
• the acetone conversion was 64.0%.
• Example 1 Therefore, as in Example 1, the supply of the reaction raw material was stopped, the flow direction of the liquid was reversed, and only the phenol raw material was supplied to the reactor at a flow rate of 15 tZh for 3 hours with an up flow (up flow).
• the catalyst layer was fluidized at a reaction temperature of 69.0 ° C.
• the supply of reaction raw materials was resumed, and the reaction was started down-flow.
• the temperature at measuring point 1 at 6 hours after the start of the reaction is 68.3 ° C
• the temperature at measuring point 2 is 68.3 ° C
• the temperature at the reactor outlet (measuring point 0) is 67.4 ° C. there were. That is, the temperature difference between measurement point 1 and measurement point 0 was 0.9 ° C, and the temperature difference between measurement point 2 and measurement point 0 was 0.9 ° C.
• the acetone conversion at this time was 72.5%.
• the bottom radius of reactor 1 is 3.3m, and 15% of the sulfonic acid groups are 2- (4pyridyl) ethanethiol so that the catalyst layer height is 3.2m (catalyst amount: 110m 3 ).
• the modified sulfonic acid type cation exchange resin catalyst was packed.
• Two thermocouple thermometers 5 were installed in the catalyst layer.
• the fixed bed reactor 1 was able to reverse the flow direction of the reaction liquid using valves 81 to 84, and the minimum fluidization feed rate was 18.8 tZh.
• a mixed raw material of phenol raw material lOOtZh and acetone raw material 3.5tZh used in Example 1 is fed in a downward flow (down flow) at a temperature of 60.0 ° C.
• a continuous reaction was started under adiabatic conditions.
• the acetone conversion rate was 98.0% after 10 hours from the start of the reaction (when the reaction was stable).
• the temperature at measuring point 1, the temperature at measuring point 2, and the temperature at the reactor outlet (measuring point 0) were all equal to 78.7 ° C.
• the temperature at measurement point 1 is 74.6 ° C
• the temperature at measurement point 2 is 74.6 ° C
• the temperature at the reactor outlet (measurement point 0) is 76.C. 6 ° C. That is, the absolute value of the temperature difference between measurement point 1 and measurement point 0 was 2.0 ° C, and the absolute value of the temperature difference between measurement point 2 and measurement point 0 was 2.0 ° C.
• the acetone conversion was 87.0%.
• valves 81 and 82 are closed, valves 83 and 84 are opened, and only the phenol raw material is pumped up through lines 91 and 94 using pump 7 at a temperature of 67.0 ° C and a flow rate of 20 tZh for 3 hours. In 1), it was supplied to the reactor 1 to flow the catalyst bed.
• Example 2 The same operation as in Example 2 was performed, except that the reaction was not stopped and the catalyst flow operation was not performed after 9 months from the start of the operation, but the operation was continued.
• the temperature at measuring point 1 is 66.8 ° C
• the temperature at measuring point 2 is 66.8 ° C
• the temperature at the reactor outlet (measuring point 0) is 18 months after the first reaction. 72. It was 4 ° C. That is, the temperature difference between measurement point 1 and measurement point 0 was 5.6 ° C, and the temperature difference between measurement point 2 and measurement point 0 was 5.6 ° C. At this point.
• the acetone conversion was 61.0%.
• Example 1 Therefore, as in Example 1, the nozzles 81 and 82 were closed, the valves 83 and 84 were opened, and only the phenol raw material was fed through the lines 91 and 94 using the pump 7 at a temperature of 65.0 °. C, flow rate
• the catalyst layer was fluidized by supplying the reactor 1 with an upward flow (upflow) at 20 tZh for 3 hours. The supply of the reaction raw material was restarted, and the reaction was started in a downward flow (down flow). At 10 hours after the start of the reaction, the temperature at measuring point 1 is 72.7 ° C, the temperature at measuring point 2 is 72.7 ° C, and the temperature at the reactor outlet (measuring point 0) is 73.5 ° C. Met. That is, the absolute value of the temperature difference between measurement point 1 and measurement point 0 is 0.8. The absolute value of the temperature difference between C, measuring point 2 and measuring point 0 was 0.8 ° C. The acetone conversion at this point was 70.5%.

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• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

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