Novel diisobutyl phthalate continuous reactor

Abstract

The utility model discloses a novel diisobutyl phthalate continuous reactor. The novel diisobutyl phthalate continuous reactor comprises a reaction kettle; an extracting agent inlet, a phthalic anhydride inlet, an isobutanol inlet, an isobutanol circulating liquid inlet and a catalyst inlet are formed in the reaction kettle, an alcohol water vapor outlet and a liquid-phase grease outlet are formed in the reaction kettle, and a plate-type separation tower I, a plate-type separation tower II, a distributor and a catalyst placing tray are arranged in the reaction kettle; according to the utility model, the double-plate type separation tower is adopted for reaction, the extraction agent is added to improve the esterification reaction efficiency, and the solid catalyst is used for reducing the corrosion to the pipe body, so that the device has the advantages of short reaction time, high reaction conversion rate, low corrosion, convenience in maintenance and the like, the energy consumption is reduced, and the product quality is improved.

Description

Technical Field

[0001] The utility model belongs to the technical field of chemical equipment, and specifically relates to a novel continuous reactor for diisobutyl phthalate. Background Art

[0002] The existing diisobutyl phthalate is produced by batch stirring reaction in a kettle. During the use process, due to uneven stirring and unstable temperature control, the reaction time for each kettle exceeds 6 hours, the reaction is incomplete, the efficiency is low, and it is easy to cause potential safety hazards during the reaction. In addition, the existing reaction kettle has a corrosion problem caused by sulfuric acid as a catalyst, often resulting in leakage of the cooling jacket of the reaction kettle, causing the esterification reaction to not proceed normally, with high energy consumption, low efficiency, cumbersome operation, and long time consumption. Summary of the Utility Model

[0003] In view of this, the technical problem to be solved by the utility model is to provide a novel continuous reactor for diisobutyl phthalate, which solves the problems of low efficiency of the stirring reaction and corrosion of the pipe body by the catalyst in the prior art.

[0004] To solve the above technical problem, the utility model discloses a novel continuous reactor for diisobutyl phthalate, comprising: a reaction kettle; an extraction agent inlet, a phthalic anhydride inlet, an isobutanol inlet, an isobutanol circulating liquid inlet, and a catalyst inlet are provided on the reaction kettle, an alcohol-water vapor outlet and a liquid-phase ester outlet are provided, a plate separation tower one, a plate separation tower two, a distributor, and a catalyst placement tray are arranged inside the reaction kettle, the alcohol-water vapor outlet is located at the top of the reaction kettle, the plate separation tower one is located in the upper part of the reaction kettle, the extraction agent inlet is located in the upper part of the plate separation tower one, the distributor is located in the lower part of the plate separation tower one, the phthalic anhydride inlet is located at the position between the plate separation tower one and the distributor, the catalyst placement tray is located below the distributor, the plate separation tower two is located below the catalyst placement tray, the isobutanol inlet and the isobutanol circulating liquid inlet are located at the position between the catalyst placement tray and the plate separation tower two, and the catalyst inlet is located on one side of the catalyst placement tray.

[0005] Further, the above plate separation tower one is formed by three guiding plates and two overflow plates arranged alternately at intervals.

[0006] Further, a flow dividing member is provided at the middle of the upper part of the above distributor, and the pipe body of the phthalic anhydride inlet is communicated with the flow dividing member.

[0007] Further, the above flow dividing member is in a hemispherical shape, its spherical surface faces upward, the top is communicated with the pipe body of the phthalic anhydride inlet, and the spherical surface is covered with liquid outlet holes.

[0008] Further, the above catalyst placement tray has an overflow tray, and a retaining ring plate is arranged in the middle of the overflow tray, and the height of the retaining ring plate is higher than the height of the overflow baffle at the edge of the overflow tray.

[0009] Furthermore, the above-mentioned distributor is cylindrical, with a plurality of conical grooves provided on its upper end face. Through holes are provided on the bottom surface of the conical grooves, and the through holes extend to the lower end face. The through holes are conical holes.

[0010] Compared with the prior art, the present application can achieve the following technical effects:

[0011] The utility model adopts a double-plate separation tower reaction, adds an extractant to improve the efficiency of the esterification reaction, and uses a solid catalyst to reduce the corrosion of the pipe body. Therefore, it has the advantages of short reaction time, high reaction conversion rate, low corrosivity, and convenient maintenance, reduces energy consumption, and improves product quality.

[0012] Of course, it is not necessary for any product implementing the present application to achieve all the above-mentioned technical effects simultaneously. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] The drawings described herein are used to provide a further understanding of the present application, and constitute a part of the present application. The schematic embodiments of the present application and their descriptions are used to explain the present application, and do not constitute an improper limitation to the present application. In the drawings:

[0014] Figure 1 is a schematic diagram of a reaction kettle according to an embodiment of the utility model.

[0015] REFERENCE SIGNS

[0016] Reaction kettle 1, extractant inlet 2, phthalic anhydride inlet 3, isobutanol inlet 4, isobutanol circulating liquid inlet 5, catalyst inlet 6, alcohol-water vapor outlet 7, liquid-phase fat outlet 8, plate separation tower one 9, plate separation tower two 10, distributor 11, catalyst placement tray 12, guide plate 13, overflow plate 14, shunt member 15, overflow tray 16, retaining ring plate 17, conical groove 18, through hole 19. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0017] The following will be combined with the drawings and embodiments to detail the implementation manner of the present application, so as to fully understand how the present application uses technical means to solve technical problems and achieve the realization process of technical effects and implement accordingly.

[0018] Please refer to Figure 1 , Figure 1 is a schematic diagram of a reaction kettle according to an embodiment of the utility model.

[0019] A novel continuous phthalic acid diisobutyl ester reactor, comprising: a reaction kettle 1; an extractant inlet 2, a phthalic anhydride inlet 3, an isobutanol inlet 4, an isobutanol circulating liquid inlet 5 and a catalyst inlet 6 are provided on the reaction kettle 1, an alcohol-water vapor outlet 7 and a liquid-phase fat outlet 8 are provided, a plate separation tower 9, a plate separation tower 10, a distributor 11 and a catalyst placement tray 12 are provided inside the reaction kettle 1, the alcohol-water vapor outlet 7 is located at the top of the reaction kettle 1, the plate separation tower 9 is located in the upper part of the reaction kettle 1, the extractant inlet 2 is located in the upper part of the plate separation tower 9, the distributor 11 is located in the lower part of the plate separation tower 9, the phthalic anhydride inlet 3 is located at the position between the plate separation tower 9 and the distributor 11, the catalyst placement tray 12 is located below the distributor 11, the plate separation tower 10 is located below the catalyst placement tray 12, the isobutanol inlet 4 and the isobutanol circulating liquid inlet 5 are located at the position between the catalyst placement tray 12 and the plate separation tower 10, and the catalyst inlet 6 is located on one side of the catalyst placement tray 12.

[0020] The plate separation tower 9 is formed by three guiding plates 13 and two overflow plates 14 arranged alternately at intervals; the plate separation tower 9 and the plate separation tower 10 have the same structure; a shunt member 15 is provided in the middle of the upper part of the distributor 11, the pipe body of the phthalic anhydride inlet 3 is communicated with the shunt member 15, the shunt member 15 is in a hemispherical shape, its spherical surface faces upward, the top is communicated with the pipe body of the phthalic anhydride inlet 3, and the spherical surface is covered with liquid outlet holes; the catalyst placement tray 12 has an overflow tray 16, a retaining ring plate 17 is provided in the middle of the overflow tray 16, and the height of the retaining ring plate 17 is higher than the height of the overflow baffle at the edge of the overflow tray 16; the distributor 11 is cylindrical, a plurality of conical grooves 18 are provided on the upper end surface, through holes 19 are provided on the bottom surface of the conical grooves 18, the through holes 19 extend to the lower end surface, and the through holes 19 are conical holes.

[0021] The esterification process in the production of dibutyl phthalate: The equipment includes a reaction kettle, a condenser, a separation tower and a water separator. During production, a quantitative amount of phthalic anhydride and a catalyst are put into the esterification kettle at one time, and the raw material butanol is added in several times according to the reaction conditions. The temperature is raised and the normal butanol reflux is maintained. The water and butanol formed by the reaction form an azeotropic vapor and enter the separation tower from the reaction kettle. After the entrained liquid is separated in the separation tower, it enters the condenser. After the vapor is completely condensed, it enters the water separator (water is in the lower layer and butanol is in the upper layer), and the water is discharged in time. The butanol returns to the reaction kettle again. During the reaction process, the acid value of the material should be measured frequently. When the acid value of the material in the kettle is less than 3.5 mg / g (KOH), the reaction is completed.

[0022] The extractant flows into the plate separation column 9 from the extractant inlet 2. The extractant slowly flows into the distributor 11 and mixes with the phthalic anhydride flowing in from the phthalic anhydride inlet 3, and then flows into the catalyst placement tray 12. The fixed catalyst in the retaining ring plate 17 continues to mix and react with the mixed liquid. After the liquid level is higher than the retaining ring plate 17, it flows into the overflow tray 16. When the overflow tray 16 is full, it flows into the plate separation column 10. At the same time, the isobutanol inlet 4 and the isobutanol circulating liquid inlet 5 connected to the water separator flow into the isobutanol to react with the mixed liquid. The generated water and butanol form an azeotropic vapor and enter the separation column from the reaction kettle. After the entrained liquid is separated in the separation column, it enters the condenser. After all the steam is condensed, it enters the water separator (water is in the lower layer and butanol is in the upper layer). The water is discharged in time, and the butanol returns to the reaction kettle to continue the reaction.

[0023] In summary, the utility model adopts a double-plate separation column for reaction, adds an extractant to improve the efficiency of the esterification reaction, and uses a solid catalyst to reduce the corrosion of the pipe body. Therefore, it has the advantages of short reaction time, high reaction conversion rate, low corrosivity, and convenient maintenance, reduces energy consumption, and improves product quality.

[0024] The above description shows and describes several preferred embodiments of the utility model. However, as mentioned above, it should be understood that the utility model is not limited to the form disclosed herein, should not be regarded as excluding other embodiments, but can be used in various other combinations, modifications, and environments, and can be changed within the scope of the utility model concept described herein through the above teachings or the technology or knowledge in related fields. And any changes and modifications made by those skilled in the art without departing from the spirit and scope of the utility model should be within the protection scope of the appended claims of the utility model.

Claims

1. A novel continuous phthalic acid diisobutyl ester reactor, comprising: Reactor; It is characterized in that the reactor is provided with an extractant inlet, a phthalic anhydride inlet, an isobutanol inlet, an isobutanol circulating liquid inlet and a catalyst inlet, and an alcohol-water vapor outlet and a liquid-phase fat outlet are provided. A plate separation tower I, a plate separation tower II, a distributor and a catalyst placement tray are arranged in the reactor. The alcohol-water vapor outlet is located at the top of the reactor. The plate separation tower I is located in the upper part of the reactor. The extractant inlet is located in the upper part of the plate separation tower I. The distributor is located in the lower part of the plate separation tower I. The phthalic anhydride inlet is located at the position between the plate separation tower I and the distributor. The catalyst placement tray is located below the distributor. The plate separation tower II is located below the catalyst placement tray. The isobutanol inlet and the isobutanol circulating liquid inlet are located at the position between the catalyst placement tray and the plate separation tower II. The catalyst inlet is located on one side of the catalyst placement tray.

2. The novel continuous reactor for diisobutyl phthalate according to claim 1, wherein The plate separation tower I is formed by three guide plates and two overflow plates arranged alternately and spaced apart from each other.

3. The novel continuous dibutyl phthalate reactor according to claim 1, characterized in that, A flow dividing member is provided in the middle of the upper part of the distributor, and the pipe body of the phthalic anhydride inlet is communicated with the flow dividing member.

4. The novel continuous dibutyl phthalate reactor according to claim 3, characterized in that, The flow dividing member is in the shape of a hemisphere with its spherical surface facing upward. The top is communicated with the pipe body of the phthalic anhydride inlet, and the spherical surface is covered with liquid outlet holes.

5. The novel continuous dibutyl phthalate reactor according to claim 1, characterized in that The catalyst placement tray has an overflow tray, and a retaining ring plate is arranged in the middle of the overflow tray. The height of the retaining ring plate is higher than the height of the overflow baffle at the edge of the overflow tray.

6. The novel continuous dibutyl phthalate reactor according to claim 1, characterized in that, The distributor is cylindrical, and a plurality of conical grooves are provided on the upper end surface. Through holes are provided on the bottom surface of the conical grooves and extend to the lower end surface. The through holes are conical holes.

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