JP3238259U - Enhanced reaction system for selectively hydrogenating benzene to produce cyclohexanone - Google Patents

Abstract

Kind Code: A1 An enhanced reaction system for selectively hydrogenating benzene to produce cyclohexanone according to the utility model increases the mass transfer area between hydrogen gas and a liquid phase material, improves the reaction efficiency, and increases the reaction efficiency. Reduce temperature and pressure, improve overall system safety and stability. The enhanced reaction system of the present invention includes a hydrogenation reactor, the hydrogenation reactor is provided with an outlet connected to a catalyst separator for separating the catalyst in the reaction product, and the gas is The bottom of the liquid separator is provided with an alcohol ketone liquid outlet connected to the cyclohexanone rectification column to separate cyclohexanone, and the side wall of the hydrogenation reactor is equipped with a A first raw material inlet provided with a first micro-interface generator was provided, and the sidewall of the addition reactor was provided with a second micro-interface generator for dispersing and pulverizing the gas into bubbles. A second feedstock inlet is provided. [Selection drawing] Fig. 1

Description

The present invention belongs to the technical field of micro-interface strengthening reaction, and specifically relates to a strengthening reaction system for selectively hydrogenating benzene to produce cyclohexanone.

Cyclohexanone is very widely used as a chemical raw material and plays an important role in industrial production and daily life. It is divided into two types, amide and non-amide, depending on its use, 70% of which is for amide. Nylon 6 and Nylon 66, which are cyclohexanone and are used in most of the amount of cyclohexanone and are often used by people, are manufactured with cyclohexanone for amide, and cyclohexanone has high solubility and low volatility. Since it has characteristics, it can also be used as an organic solvent. As can be seen from the above, cyclohexanone has become a very important chemical raw material in industrial production, especially in the polyamide industry.

Selective hydrogenation of benzene to produce cyclohexanone is the latest method for producing cyclohexanone, which mainly produces cyclohexene by the hydrogenation reaction of benzene. In this process, benzene is used as a raw material. Cyclohexene is produced by selectively hydrogenating under the catalyst of a ruthenium-supported catalyst, and cyclohexene and acetic acid are esterified under the action of a solid acid catalyst to produce cyclohexyl acetate. The produced cyclohexanol acetate and hydrogen are subjected to an addition reaction with a ketone catalyst to produce acetic acid and cyclohexanol, and this cyclohexanol is dehydrogenated under the action of a dehydrogenation catalyst to produce cyclohexanone. This process has high conversion and selectivity, with little waste liquid, waste air and solid waste generation, and high atomic economy. In addition, compared to the cyclohexene hydration method, the cyclohexane / cyclohexene separation step is omitted, and energy consumption is significantly reduced. And the by-product ethanol can be used for the production of other chemical industries, increasing the added value of the product and increasing the profit. However, although there are clear process advantages to selectively hydrogenating benzene to produce cyclohexanone, there are some defects. On the other hand, the mass transfer area of the gas-liquid phase of the existing hydrogenation reactor and the addition reactor is limited, and the material of hydrogen and the liquid phase cannot be sufficiently mixed during the reaction, and the mass transfer between the gas-liquid phase is not possible. Low efficiency, low reaction efficiency, high energy consumption, and on the other hand, high temperature and pressure in the reactor significantly reduce the safety and stability of the entire system.

In consideration of the above, the present invention is proposed.

In view of this, the first object of the present invention is to provide an enhanced reaction system for selectively hydrogenating benzene to produce cyclohexanone, which is a reaction system of a hydrogenation reactor and an addition reactor. A micro-interface generator is provided at the inlet of the raw material. On the other hand, by installing a micro-interface generator, hydrogen gas is dispersed and crushed into microbubbles at the micron diameter level, and the hydrogen gas and the liquid phase material are separated. Increase the phase interface area between them, make the material movement space sufficient, increase the residence time of hydrogen gas in the liquid phase, reduce the consumption of hydrogen gas, greatly improve the reaction efficiency, and improve the reaction process. It significantly reduces energy consumption and, on the other hand, lowers the temperature and pressure inside the reactor, improving the safety and stability of the entire system.

A second object of the present invention is to provide a method for producing cyclohexanone using the above-mentioned strengthening reaction system, in which the operating conditions are milder, the reaction temperature and the reaction temperature are ensured while ensuring the reaction efficiency. The pressure is reduced, the safety is high, the energy consumption is low, and a better reaction effect than before can be obtained.

In order to achieve the above object of the present invention, the following technical solutions are specifically adopted. The present invention provides an enhanced reaction system for preparing cyclohexanone by selective hydrogenation of benzene, including a hydrogenation reactor; the hydrogenation reactor is equipped with an emission port and the emission port is a reaction generation. Connected to a catalyst separator for use with catalysts in objects. Separated; oil phase outlet is provided at the top of the catalyst separator, and the oil phase outlet is connected to an esterification reactor for esterification of cyclohexene and acetic acid; cyclohexyl acetate outlet on the side wall. And cyclohexene are provided. The acetate outlet is connected to an addition reactor for the addition reaction of cyclohexanol acetate and hydrogen; the bottom of the addition reactor is equipped with a mixture outlet, so the mixture outlet is ethanol rectification for separating ethanol. It is connected to a tower; the ethanol rectification column is equipped with a heavy component outlet, and the heavy component outlet is connected to a cyclohexanol rectification column to separate the gas phase cyclohexanol; cyclohexanol rectification. The upper part of the tower is equipped with a gas phase outlet and a gas phase outlet. Is connected to a dehydrogenation reactor for performing cyclohexanol dehydrogenation reactions. The side wall of the dehydrogenation reactor is provided with a product outlet, which is connected to a gas-liquid separator for separating hydrogen. The bottom of the gas and liquid. The separator is provided with an alcohol-ketone solution outlet, and the alcohol-ketone solution outlet is connected to a cyclohexanone rectification column for separating cyclohexanone. A first raw material inlet is provided on the side wall of the hydrogenation reactor, and a first microinterface generator for dispersing the broken gas in bubbles is provided at the first raw material inlet, and the addition reactor is provided. The side wall is equipped with a first micro-interface generator, and the second raw material inlet is equipped with a second micro-interface generator to disperse the broken gas into air bubbles.

In the prior art of the invention, the reaction for selectively hydrogenating benzene to produce cyclohexanone has the following problems. On the one hand, the mass transfer area of the gas-liquid phase of the existing reactor is limited, the reaction mixing raw material and hydrogen gas cannot be sufficiently mixed during the reaction, the energy consumption is high and the reaction efficiency is low, and on the other hand. Since the temperature and pressure during the reaction are too high, the safety and stability of the entire system cannot be ensured. In the enhanced reaction system for selectively hydrogenating benzene of the present invention to produce cyclohexanone, a micro-interface generator is provided at the raw material inlet of the hydrogenation reactor and the addition reactor, while hydrogen gas is produced at the micron level in diameter. Disperses and crushes into microbubbles, increases the phase interface area between hydrogen gas and liquid phase material, makes the material movement space sufficient, and further increases the residence time of hydrogen gas in the liquid phase, hydrogen gas. The gas consumption is reduced, the reaction efficiency is greatly improved, the energy consumption of the reaction process is significantly reduced, and on the other hand, the temperature and pressure in the reactor are lowered, and the safety and stability of the whole system are increased.

Further, in order to recycle the catalyst into a hydrogenation reactor for recycling, a catalyst outlet is provided at the bottom of the catalyst separator. By returning the recovered catalyst to the hydrogenation reactor and reusing it, the loss of the catalyst can be reduced, and the catalyst can be continuously taken out, regenerated, or replenished, and has high activity and high selection. It maintains its properties, which enables continuous and stable production over a long period of time.

Further, a static solution outlet is provided at the bottom of the cyclohexanol rectification column, and the static solution outlet is connected to an esterification reactor to recycle unreacted cyclohexyl acetate. The reaction product after the esterification reaction contains a small amount of unreacted cyclohexyl acetate, and after undergoing ethanol rectification and cyclohexanol rectification, it flows out from the outlet of the kettle solution and is returned to the esterification reactor for the esterification reaction. As we re-participate in, the utilization rate of raw materials will be sufficiently improved.

Further, a hydrogen outlet is provided on the upper part of the gas-liquid separator, and the hydrogen outlet is connected to a second microinterface generator for recycling the separated hydrogen. The product after the cyclohexanol dehydrogenation reaction contains a large amount of hydrogen gas, and this hydrogen gas can be recovered by a gas-liquid separator to sufficiently increase the utilization rate of the hydrogen gas. Preferably, the hydrogen outlet is provided with a hydrogen compressor for compressing hydrogen before recovering and using it.

Further, the first microinterface generator and the second microinterface generator are both pneumatic microinterface generators, and the number of settings of both the first microinterface generator and the second microinterface generator is at least. One or more.

Further, there are no restrictions on the installation method, installation position, and number of the first micro-interface generator and the second micro-interface generator, and more preferably, the number of the micro-interface generators is one or more, and the reaction is carried out. The micro-interface generators, which are arranged in order from top to bottom in front of the vessel and are arranged in multiple rows in this way, can simultaneously disperse and crush the inflowing hydrogen gas, making the subsequent reaction efficiency more effective. Can be improved.

As will be appreciated by those skilled in the art, the micro-interface generators employed in the present invention include prior patents of the present invention, such as application numbers CN2016106441119.6, 201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN207581700U. It has already been embodied in the patent of. In the prior patent CN2016106441119.6, the specific product structure and operating principle of the micron bubble generator (that is, the microinterface generator) are introduced in detail, and the application document states that the micron bubble generator is the main body. Including the secondary crushing member, the main body has a cavity, the main body is provided with an inlet communicating with the cavity, and both the opposite first end and the second end of the cavity are open. The cross-sectional area of the cavity decreases from the middle of the cavity towards the first and second ends of the cavity, and secondary crushing members are provided at at least one of the first and second ends of the cavity. A part of the secondary crushing member is provided in the cavity, and an annular passage is formed between the secondary crushing member and the through holes opened at both ends of the cavity. The micron bubble generator is an intake pipe and a supply. Further includes a liquid tube. " From the specific structure disclosed in the application documents, it can be seen that the specific operating principle is as follows. The liquid enters the micron bubble generator along the tangential direction through the liquid supply pipe, rotates at ultra-high speed to cut the gas, and crushes the gas bubbles into microbubbles at the micron level. The mass transfer area between the phase and the gas phase is increased, and the micron bubble generator in this patent belongs to the pneumatic microinterface generator.

Further, in the prior patent 201610641251.7, the primary bubble crusher has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble crusher communicates the supply port and the gas-liquid mixture outlet. It is stated that the bubble crusher requires gas-liquid mixing, and as can be seen from the later drawings, the primary bubble crusher mainly uses the circulating fluid as a power source. Actually, the primary bubble crusher is a hydraulic micro interface generator, and the secondary bubble crusher simultaneously introduces a gas-liquid mixture into an elliptical rotating sphere and rotates it to crush bubbles in the process of rotation. The secondary bubble crusher is actually a pneumatic hydraulic hybrid micro interface generator. Actually, both the hydraulic micro-interface generator and the pneumatic-hydraulic hybrid micro-interface generator are specific forms of the micro-interface generator, but the micro used in the present invention is used. The interface generator is not limited to some of the above-mentioned forms, and the specific structure of the bubble crusher described in the prior patent is only one of the forms that can be adopted by the micro-interface generator of the present invention. do not have.

In addition, the prior patent 201710766435.0 describes that "the principle of the bubble crusher is to collide gas with each other with a high-speed jet", and it is also described that it can be used for a micro interface strengthening reactor. , The relationship between its own bubble crusher and the micro interface generator has been verified, and the prior patent CN106187660 also has a description related to the specific structure of the bubble crusher. Explains in detail the specific operating principle of the bubble crusher S-2 with reference to the paragraphs [0031]-[0041] of the specification and the part of the drawing, and the top of the bubble crusher is of the liquid phase. It is the inlet, the side is the inlet of the gas phase, and by providing suction through the liquid phase coming in from the top, it achieves the effect of crushing into ultrafine bubbles, and as you can see from the drawing, the bubble crusher. Has a tapered structure, the upper diameter is larger than the lower diameter, in order to provide better suction to the liquid phase.

In the early stage of the prior patent application, the micro interface generator was just developed, so it was named as a micron bubble generator (CN2016106441119.6), a bubble crusher (201710766435.0), etc. In the latter period, the name was changed to the micro interface generator, and at present, the micro interface generator in the present invention corresponds to the former micro bubble generator, bubble crusher, etc., but the name is different.

As described above, the micro-interface generator of the present invention belongs to the prior art, and among the bubble crushers, the pneumatic bubble crusher, the hydraulic bubble crusher type, and the pneumatic-hydraulic hybrid bubble crusher type are also available. Although there is, the type is mainly selected according to the specific operating conditions, and the connection between the micro interface generator and the reactor and other equipment depends on the structure of the micro interface generator, including the connection structure and connection position. Unlike, it is not limited here.

Further, a benzene purifier for purifying the raw material benzene is also included, a purified benzene outlet is provided at the bottom of the benzene purifier, and the purified benzene outlet is connected to the first microinterface generator. .. A desulfurization adsorbent packing layer is provided in the benzene purifier capable of purifying the raw benzene in order to remove sulfur-containing impurities in the raw benzene, and the sulfur content of benzene from the benzene purifier is 5PPb or less. Therefore, catalyst poisoning due to impurities in the raw material benzene is avoided.

In addition, it also includes a cyclohexanone reflux tank, the bottom of the cyclohexanone reflux tank equipped with a reflux pipeline for returning a portion of cyclohexanone to the cyclohexanone rectification column. A reflux pump is provided in the reflux conduit. A part of the condensed liquid in the cyclohexanone reflux tank is pressurized by the reflux pump and then refluxed into the cyclohexanone rectification column through the reflux conduit to take in the excess heat at the top of the cyclohexanone rectification column. The recovery purity of cyclohexanone can also be improved by maintaining the thermal balance of the entire column and undergoing multiple refluxs. By adjusting the amount of reflux using a reflux pump as compared with the natural reflux, the amount of reflux can be stabilized and the operability can be improved.

In addition, both the hydrogenation reactor and the addition reactor are fixed bed catalytic reactors. Since the catalyst inside the fixed-bed catalyst reactor is directly filled in the fixed bed, it is not easily worn in the floor, can be used for a long period of time, has a simple structure, and is easy to handle.

In addition, the utility model provides a method for preparing cyclohexanone by selective hydrogenation of benzene. This includes the following steps: After hydrogen is dispersed and decomposed into microbubbles, a reaction product is obtained through a catalytic hydrogenation reaction with benzene and an esterification reaction with acetic acid. Hydrogen dispersed and decomposed with the reaction product continues the addition reaction and dehydrogenates. In addition, the crude benzene is first purified by a benzene refiner and then delivered to the interior of the first microinterface generator, while at the same time hydrogen is passed through the interior of the first microinterface generator, whereby the diameter. It is broken down into micron microbubbles, hydrogen is dispersed and broken down into microbubbles, then completely emulsified with benzene, the emulsion enters the hydrogenation reactor for the hydrogenation reaction, and the reaction product is catalytically separated. Enter the catalyst separator for. The separated catalyst is returned to the hydrogenation reactor and reused. After removing the catalyst, cyclohexene enters the esterification reactor and undergoes an esterification reaction with acetic acid under the action of the catalyst, and cyclohexene acetate, which is an esterification product, enters the inside. It enters the addition reactor of the second microinterface generator and causes an addition reaction by the action of the catalyst. The product is separated by ethanol before entering the cyclohexanol rectification column, the gas phase cyclohexanol enters the interior of the dehydrogenation reactor for the dehydrogenation reaction reaction, and at the same time the unreacted bottom of the cyclohexanol rectification column. Cyclohexanol acetate is returned to the addition reactor and reused to put the dehydrogenation product in a gas-liquid separator to separate hydrogen, while at the same time a second microinterface generator for reusing the separated hydrogen, and hydrogen. After separation, the alcohol and ketone solution finally enter cyclohexane. Separation and collection of cyclohexanone is carried out in a ketone distillation column.

The temperature of the hydrogenation reactor is 115 to 138 ° C., the pressure is 2.1 to 2.6 MPa, the temperature of the addition reactor is 185 to 210 ° C., and the pressure is 2.2 to 3.1 MPa.

Compared to the prior art, the beneficial effects of the current utility model are: In the enhanced reaction system for selectively hydrogenating benzene of the present invention to produce cyclohexanone, by providing micro-interface generators at the raw material inlets of both the hydrogenation reactor and the addition reactor, on the one hand, the hydrogen gas is calibrated. Dispersed into microbubbles at the micron level and crushed to increase the phase interface area between hydrogen gas and liquid phase material, to provide sufficient space for mass transfer, and to increase the residence time of hydrogen gas in the liquid phase. It reduces the consumption of hydrogen gas, greatly improves the reaction efficiency, significantly reduces the energy consumption of the reaction process, and on the other hand lowers the temperature and pressure inside the reactor, improving the safety and stability of the whole system. Improve.

It is a structural schematic diagram of the strengthening reaction system which produces cyclohexanone by selectively hydrogenating benzene provided in the Example of this invention.

Reading the following detailed description of the preferred embodiments will reveal to those skilled in the art various other advantages and advantages. The drawings are intended only to illustrate preferred embodiments and should not be considered limiting the invention. Also, the same components are indicated by the same reference numbers throughout the drawing.

The technical solutions of the present invention will be described clearly and completely below with reference to the accompanying drawings and specific embodiments, although those skilled in the art will appreciate that the embodiments described below are embodiments of the present invention. Understand that some, but not all. The examples are used only to illustrate the invention of the invention and should not be considered as limiting the scope of the invention of the invention. All other embodiments obtained by one of ordinary skill in the art based on the embodiments of the present invention are included in the scope of protection of the present invention. If the examples do not indicate specific conditions, follow the conventional conditions or the conditions recommended by the manufacturer. Reagents or equipment used without manufacturer's instructions are traditional products that can be purchased from the market.

Note the terms "center", "top", "bottom", "left", "right", "vertical", "horizontal", "inside" and "outside" in the description of the present invention. The orientation or positional relationship shown by, etc. is based on the orientation or positional relationship shown in the accompanying drawings, which describes or implies the present invention, rather than indicating or implying a referenced device or element. It is for convenience only to simplify the explanation. It must have a particular orientation and therefore it should not be construed as a limitation on the invention of the present invention. In addition, the terms "1st", "2nd", and "3rd" are used for explanatory purposes only and should not be construed as implying or implying relative importance. ..

In order to more clearly explain the technical solution of the present invention, the following description is given in the form of specific embodiments.

As shown in FIG. 1, the enhanced reaction system for selectively hydrogenating benzene according to the embodiment of the present invention to produce cyclohexanone includes a hydrogenation catalyst 10, and the hydrogenation catalyst 10 contains a reaction product. A discharge port 11 connected to the catalyst separator 20 is provided to separate the catalyst inside, and the catalyst is collected and placed in the hydrogenation reactor 10 at the bottom of the catalyst separator 20. A catalyst outlet 21 is provided for circulation use, and the recovered catalyst is returned to the inside of the hydrogenation reactor 10 and reused, so that the loss of the catalyst can be reduced and the catalyst can be continuously taken out. It can be regenerated and replenished to maintain high activity and high selectivity, which enables continuous and stable production over a long period of time.

An oil phase outlet 22 connected to an esterification reactor 30 for esterifying cyclohexene and acetic acid is provided at the top of the catalyst separator 20, and the side wall of the esterification reactor 30 is provided with an oil phase outlet 22. The cyclohexyl acetate outlet 31 connected to the addition reactor 40 is provided for the addition reaction between cyclohexyl acetate and hydrogen.

The side wall of the hydrogenation reactor 10 is provided with a first raw material inlet 12 provided with a first micro-interface generator 101 for dispersing gas in bubbles and pulverizing the gas. On the side wall of the reactor 40, a second raw material inlet 41 provided with a second micro-interface generator 401 for dispersing the gas in bubbles and pulverizing the gas is provided. Preferably, the first micro-interface generator 101 and the second micro-interface generator 401 are both pneumatic micro-interface generators.

Further, a mixture outlet 42 connected to an ethanol rectification column 50 for separating ethanol is provided at the bottom of the addition reactor 40, and cyclohexanol is provided at the bottom of the ethanol rectification column 50. A heavy component outlet 51 connected to the rectification column 60 is provided, and the esterification reactor 30 is provided at the bottom of the cyclohexanol rectification column 60 in order to return and reuse unreacted cyclohexyl acetate. A kettle liquid outlet 61 is provided, and a gas phase outlet 62 connected to a dehydrogenator 70 for dehydrogenizing cyclohexanol is provided at the top of the cyclohexanol rectification column 60. Is provided.

Specifically, the side wall of the dehydrogenation reactor 70 is provided with a product outlet 71 connected to the gas-liquid separator 80 for separating hydrogen gas, and the bottom of the gas-liquid separator 80 is provided. Is provided with an alcohol ketone liquid outlet 81 connected to a cyclohexanone rectification column 90 for separating cyclohexanone, and the separated hydrogen is returned to the top of the gas-liquid separator 80 for reuse. Is provided with a hydrogen outlet 82 connected to the second micro-interface generator 401.

Further, this embodiment further includes a benzene purifier 100 for purifying raw benzene, and a purified benzene outlet 110 connected to a first micro-interface generator 101 is provided at the bottom of the benzene purifier 100. Has been done.

The above embodiment further comprises a cyclohexanone recirculation tank 120 provided at the bottom with a perfusion tube that returns a portion of cyclohexanone back into the cyclohexanone rectification column.

In the above embodiment, the hydrogenation reactor 10 and the addition reactor 40 are both fixed-bed catalyst reactors. Since the catalyst in the fixed bed catalyst reactor is directly filled in the fixed bed, it is not easily worn in the floor, can be used for a long period of time, has a simple structure, and is easy to handle.

In the following, the operating process and principle of the enhanced reaction system for selectively hydrogenating the benzene of the present invention to produce cyclohexanone will be briefly described.

The crude benzene is purified by the benzene purifier 100 and then enters the inside of the first micro-surface generator 101, and at the same time, the hydrogen gas is introduced into the inside of the first micro-surface generator 101, and the micro has a diameter of micron level. It is crushed into bubbles, hydrogen gas is dispersed in microbubbles and crushed, and then sufficiently emulsified with benzene. The catalyst is separated from the catalyst separator 20 from the 11th, and the separated catalyst is re-injected into the hydrogenation reactor 10 from the catalyst discharge port 21 and used for circulation. The cyclohexene from which the catalyst has been removed enters the esterification reactor 30 and undergoes an esterification reaction with acetic acid under the action of the catalyst, and cyclohexyl acetate, which is an esterification product, is generated at the second micro interface from the cyclohexyl acetate outlet 31. Entering the interior of the device 401, at the same time the hydrogen gas is introduced into the second micro interface generator 401, crushed into microbubbles at the micron diameter level, the hydrogen gas is fully emulsified with cyclohexyl acetate, and then the emulsion It enters the addition reactor 40 and undergoes an addition reaction under the action of a catalyst, the product enters the ethanol rectification tower 50 from the mixture outlet 42, ethanol is separated, and the mixture from which ethanol is separated is cyclohexanol rectification. Recharged into the column 60, the vapor phase cyclohexanone enters the dehydrogenation reactor 70 via the gas phase outlet 62 and undergoes a dehydrogenation reaction, while the unreacted cyclohexyl acetate undergoes an addition reaction via the kettle liquid outlet 61. It is returned to the vessel 40 and reused, and the product after dehydrogenation enters the gas-liquid separator 80 to separate the hydrogen gas, and the separated hydrogen gas generates a second micro interface through the hydrogen gas outlet 82. The alcohol ketone solution returned to the apparatus 401 and reused, and the hydrogen gas is separated, enters the cyclohexanone rectification column 90 via the alcohol ketone solution outlet 81, and the cyclohexanone is separated and recovered.

Finally, it should be noted that the above embodiments are used only to illustrate the technical solutions of the present invention and are not limiting them. One of ordinary skill in the art needs to understand: It is still the technical solution recorded in the aforementioned embodiment may be modified or some or all of its technical features may be equally replaced. .. These modifications or replacements do not form the essence of the corresponding technical solution. It deviates from the scope of the technical solution of the embodiment of the present invention.

10-Hydrogen reactor; 11-Discharge port; 12-1st raw material inlet; 101-1st micro interface generator;
20-catalyst separator; 21-catalyst outlet; 22-oil phase outlet;
30-Esterification reactor; 31-Cyclohexyl acetate outlet;
40-Addition reactor; 41-second raw material inlet; 42-mixture outlet; 401-second micro interface generator;
50-Ethanol rectification tower; 51-Heavy component outlet;
60-Cyclohexanol rectification column; 61-Kama liquid outlet; 62-Vaic phase outlet;
70-dehydrogenation reactor; 71-product outlet;
80-gas-liquid separator; 81-alcohol ketone liquid outlet; 82-hydrogen gas outlet;
90-Cyclohexanone rectification column;
100-Benzene Purifier; 110-Purified Benzene Outlet;
120-Cyclohexanone reflux tank.

Claims (8)

An enhanced reaction system that selectively hydrogenates benzene to produce cyclohexanone.
The hydrogenation reactor includes a hydrogenation reactor, the hydrogenation reactor is provided with a discharge port connected to the catalyst separator for separating the catalyst in the reaction product, and the top of the catalyst separator is provided with a discharge port. An oil phase outlet connected to an esterification reactor is provided for the esterification reaction of cyclohexene and acetic acid.
The side wall of the esterification reactor is provided with a cyclohexyl acetate outlet connected to the addition reactor for addition reaction of cyclohexyl acetate and hydrogen.
The bottom of the addition reactor is provided with a mixture outlet connected to an ethanol rectification column to separate ethanol.
The bottom of the ethanol rectification column is provided with a heavy component outlet connected to the cyclohexanol rectification column in order to separate the gas phase cyclohexanol.
The top of the cyclohexanol rectification column is provided with a gas phase outlet connected to a dehydrogenation reactor to carry out the dehydrogenation reaction of cyclohexanol.
The side wall of the dehydrogenation reactor is provided with a product outlet connected to a gas-liquid separator for separating hydrogen gas.
The bottom of the gas-liquid separator is provided with an alcohol-ketone solution outlet connected to a cyclohexanone rectification column to separate cyclohexanone.
The side wall of the hydrogenation reactor is provided with a first raw material inlet provided with a first micro-interface generator for dispersing and pulverizing the gas into bubbles.
An enhanced reaction system characterized in that the side wall of the addition reactor is provided with a second raw material inlet provided with a second micro-interface generator for dispersing and pulverizing the gas into bubbles. .. The benzene according to claim 1, wherein the bottom of the catalyst separator is provided with a catalyst outlet for recovering the catalyst and putting it in the hydrogenation reactor for circulation use. A strengthening reaction system that produces cyclohexanone by hydrogenation. Claim 1 is characterized in that the bottom of the cyclohexanol rectification column is provided with a kettle liquid outlet connected to the esterification reactor in order to return and reuse unreacted cyclohexyl acetate. A fortified reaction system for selectively hydrogenating the benzene described in the above to produce cyclohexanone. The first aspect of the present invention is characterized in that the top of the gas-liquid separator is provided with a hydrogen outlet connected to the second micro-interface generator for returning and reusing the separated hydrogen. An enhanced reaction system for selectively hydrogenating the described benzene to produce cyclohexanone. The first micro-interface generator and the second micro-interface generator are both pneumatic micro-interface generators, and the number of installations of the first micro-interface generator and the second micro-interface generator is the same. The enhanced reaction system for producing cyclohexanone by selectively hydrogenating benzene according to claim 1, wherein each of them is at least one or more. A claim comprising a benzene purifier for purifying raw benzene, further comprising a purified benzene outlet connected to the first micro-interface generator at the bottom of the benzene purifier. A strengthening reaction system for producing cyclohexanone by selectively hydrogenating the benzene according to Item 1. The cyclohexanone is produced by selectively hydrogenating benzene according to claim 1, wherein a reflux channel for returning a part of cyclohexanone to the cyclohexanone rectification column further includes a cyclohexanone reflux tank provided at the bottom. Enhanced reaction system. The benzene according to any one of claims 1 to 7, wherein both the hydrogenation reactor and the addition reactor are fixed-bed catalytic reactors, to produce cyclohexanone. Enhanced reaction system.

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