A device, system and method for continuously producing cyclohexanone oxime

Abstract

The invention relates to the field of chemical technology, and in particular to a device, system and method for continuously producing cyclohexanone oxime, comprising a reactor, wherein the reactor is composed of a liquid distributor, a rotating filler, a rotating shaft, a jacket, a bottom liquid outlet, an external heat exchanger A, an external circulating pump A, an external heat exchanger B and an external circulating pump B, wherein a liquid feed port 1, a liquid feed port 2 and a liquid feed port 3 are respectively connected and arranged on the top of the liquid distributor, and the bottom end of the liquid distributor extends into a cavity of the rotating filler, and the rotating filler is fixed on the rotating shaft; the invention can significantly shorten the cyclohexanone oximation reaction time without using a co-solvent, thereby improving the reaction conversion rate, and the reaction time is short, the selectivity of cyclohexanone oxime can reach more than 99%, and a residual ammonia recovery process is provided, so that all raw materials are almost completely converted into butanone oxime and water, the raw material utilization rate is high, the material consumption is reduced, and the service life of the catalyst is also increased.

Description

Technical Field

[0001] The invention relates to the technical field of chemical industry, and in particular to a device, a system and a method for continuously producing cyclohexanone oxime. Background Art

[0002] Caprolactam is an important chemical raw material and can be used to produce nylon 6 engineering plastics, fibers, films, etc. Cyclohexanone oxime rearrangement is the current mainstream process for producing caprolactam, and the purity of cyclohexanone oxime has an important influence on the efficiency of the rearrangement process. How to produce high-purity cyclohexanone oxime with high efficiency and low consumption is one of the key links that restrict energy conservation and consumption reduction in the entire process of caprolactam production. The raw material for the production of cyclohexanone oxime is usually cyclohexanone, and the traditional production process is to directly generate cyclohexanone oxime by reacting cyclohexanone with hydroxylamine salts. This method has a tendency to be replaced by new methods due to large emissions of three wastes, heavy environmental pollution, the by-product of low-value ammonium sulfate, and insufficient atom economy. Cyclohexanone, ammonia water, and hydrogen peroxide react under the catalysis of titanium silicalite (TS-1) as follows (such as Figure 3 The direct synthesis of cyclohexanone oxime by the reaction (as shown) has many advantages such as high raw material utilization, high reaction selectivity, and environmental friendliness, and is expected to become the mainstream process for the production of cyclohexanone oxime in the future.

[0003] Theoretically, the selectivity of cyclohexanone oxime obtained by this process can be close to 100%, but when the operating conditions are not ideal, side reactions are also very likely to occur, mainly including the direct reaction of hydrogen peroxide and ammonia to produce nitrogen and nitrogen oxides, condensation of cyclohexanone to form dimers, and deep oxidation of cyclohexanone oxime by hydrogen peroxide to nitrocyclohexane.

[0004] Since cyclohexanone is immiscible with ammonia and hydrogen peroxide, an oil-water two-phase will be formed during the reaction, so that the reaction is limited by mass transfer resistance and its reaction rate is reduced. At the same time, since the reaction solution has a long residence time in the reactor and poor mixing uniformity, side reactions are allowed to occur in large quantities, and the selectivity of cyclohexanone oxime in the product is low. Therefore, current ammoximation processes generally add cosolvents such as tert-butyl alcohol, etc., so that the oil-water two-phase is miscible, mass transfer resistance and mixing difficulty are reduced, so that the reaction efficiency can be significantly improved, but this also increases the energy consumption of subsequent separation cosolvents, pushing up the production cost of cyclohexanone oxime.

[0005] Titanium silicate molecular sieve is a commonly used catalyst in this process. Its excellent catalytic performance comes from the ultra-high specific surface area brought by the porous structure. However, in actual production, due to the lipophilicity of TS-1, the generated cyclohexanone oxime is difficult to diffuse out of the catalyst pores, affecting the efficiency of the catalytic reaction. At the same time, due to the low selectivity and long reaction time of the current process, it is easy to cause high-boiling point macromolecular byproducts to coat and deposit carbon on the catalyst surface, shortening the service life of the catalyst. Summary of the invention

[0006] The object of the present invention is to provide a device, system and method for continuously producing cyclohexanone oxime, which can significantly shorten the cyclohexanone oxime reaction time without using a co-solvent, and the selectivity of cyclohexanone oxime can reach more than 99%.

[0007] To achieve the above-mentioned purpose, the present invention provides the following technical scheme: a device for continuously producing cyclohexanone oxime, comprising a reactor, wherein the reactor is composed of a liquid distributor, a rotating filler, a rotating shaft, a jacket, a bottom liquid outlet, an external heat exchanger A, an external circulation pump A, an external heat exchanger B and an external circulation pump B, wherein the top of the liquid distributor is respectively connected with liquid feed port 1, liquid feed port 2 and liquid feed port 3, the bottom end of the liquid distributor extends into the cavity of the rotating filler, the rotating filler is fixed on the rotating shaft, a bottom baffle is fixed on the surface of the rotating shaft and below the rotating filler, a sealing component is fixed at the bottom of the reactor, the bottom end of the rotating shaft is fixed to the sealing component, a motor is fixed at the bottom of the reactor, the output shaft of the motor is fixedly connected to the sealing component, and external circulation pipelines are fixed on the left and right sides of the outside of the reactor.

[0008] Preferably, the rotating filler is any one of stainless steel knitted mesh filler, stainless steel wire mesh woven filler, alumina ceramic corrugated regular filler, plastic wire mesh filler, integral silicon carbide filler or foam metal filler, and the selected rotating filler is coated with a titanium silicon molecular sieve film or other catalyst film.

[0009] Preferably, a semi-enclosed shell is fixed to the outside of the rotating filler, and a series of spoiler components are fixed to the outside of the semi-enclosed shell, and the bottom baffle is connected to the rotating shaft through a speed change gear set.

[0010] A system for continuously producing cyclohexanone oxime comprises a hydrogen peroxide inlet, a cyclohexanone inlet, an ammonia water inlet, a hot steam inlet, a wastewater outlet, a reactor, a phase separation tank, a water phase circulation pump, an evaporation tank and a cyclohexanone oxime outlet, wherein the hydrogen peroxide inlet, the cyclohexanone inlet and the ammonia water inlet are respectively connected to a first liquid feed inlet, a second liquid feed inlet and a third liquid feed inlet, the bottom liquid outlet is connected to a liquid inlet of the phase separation tank, the heavy phase outlet at the bottom of the phase separation tank is connected to the cyclohexanone oxime outlet, the upper light phase outlet of the phase separation tank is connected to a water phase circulation pump, the water phase circulation pump is connected to the liquid inlet of the evaporation tank, the hot steam inlet is connected to a gas inlet at the bottom of the evaporation tank, the liquid outlet at the bottom of the evaporation tank is connected to a wastewater outlet, and the liquid outlet at the top of the phase separation tank is connected to a pipeline of an ammonia water inlet.

[0011] Preferably, a filler or a sieve plate structure is provided in the evaporation tank.

[0012] A method for continuously producing cyclohexanone oxime, the method comprising the following steps:

[0013] Step 1: Freshly fed hydrogen peroxide liquid, cyclohexanone liquid and ammonia water are premixed in a liquid distributor and then sprayed onto a rotating packing at high speed. An oximation reaction occurs under the action of a catalyst loaded on the rotating packing. The reaction liquid sheared by the packing flows toward the wall of the reactor under the combined action of a semi-enclosed shell and a bottom baffle. The rotation of the baffle and the spoiler of the packing shell lift the liquid upward and flow through the packing again to continue the reaction. The liquid level in the reactor is controlled above the packing.

[0014] Step 2: Part of the reaction liquid in the kettle flows into the liquid distributor through an external circulation pump and an external heat exchanger, and is sprayed onto the rotating filler through the liquid distributor together with the freshly fed material. The external heat exchanger and the reactor jacket jointly remove the reaction heat. The material after sufficient reaction in the reactor is extracted from the bottom of the reactor and enters the phase separation tank. The crude cyclohexanone oxime product is extracted from the heavy phase and sent to the cyclohexanone oxime refining section, and the ammonia-containing wastewater is extracted from the light phase;

[0015] Step 3: The ammonia-containing wastewater is countercurrently contacted with hot steam in the evaporation tank, and the ammonia is fully stripped by the water vapor and dissolved into the freshly fed concentrated ammonia water; the wastewater after evaporation of the residual ammonia is sent to the wastewater treatment unit.

[0016] Preferably, in step 1, the molar ratio of ammonia water, hydrogen peroxide and cyclohexanone entering the liquid distributor is 1.1:1:1 to 1.5:1:1.

[0017] Preferably, in step 1, the pressure in the reactor is 1-10 atm, the liquid temperature is controlled at 45-150° C., the residence time in the reactor is 30-200 min, and the rotation speed of the rotating filler is between 600-2500 rpm.

[0018] Compared with the prior art, the present invention has the following beneficial effects:

[0019] 1. The reaction raw materials are sheared at high speed in the rotating filler, the oil-water two phases are fully emulsified and uniformly mixed, and are fully in contact with the catalyst, and the mass transfer resistance is reduced, so that the ammoximation reaction can be carried out quickly. Since the catalyst of the present invention is loaded on the rotating filler, the cyclohexanone oxime generated in the catalyst pores can quickly leave the pores under the action of the high-speed centrifugal force field, and the internal diffusion coefficient is greatly enhanced. At the same time, the external diffusion resistance is reduced by the stirring of the rotating filler and the automatic and passive circulation of the liquid in the kettle, and the catalytic reaction efficiency is greatly enhanced; due to the shorter residence time and more uniform mixing effect of the present invention, hydrogen peroxide always remains involved in the ammoximation reaction, and the decomposition amount is reduced. Under the combined effect of the above three factors, when the present invention is used to produce cyclohexanone oxime, cyclohexanone is almost completely converted into cyclohexanone oxime, and the conversion rate of hydrogen peroxide and ammonia water can reach more than 99.5%. Under the condition of not using a co-solvent, the reaction time is similar to the advanced level of the process using a co-solvent, so that the reaction conversion rate is improved and the reaction time is short.

[0020] 2. Cyclohexanone, hydrogen peroxide and ammonia water can be uniformly mixed in the reactor of the present invention, and the catalytic reaction efficiency is high, and the ammonia water is controlled to be slightly excessive. The above conditions ensure that cyclohexanone and hydrogen peroxide fully participate in the ammoximation reaction, reduce the occurrence of side reactions such as direct oxidation of cyclohexanone by hydrogen peroxide, cross-linking of cyclohexanone molecules, and direct oxidation of ammonia water by hydrogen peroxide to nitrogen oxides. Under the combined effect of the above factors, the selectivity of cyclohexanone oxime produced by the present invention can reach more than 99%, the concentration of cyclohexanone oxime in the crude cyclohexanone oxime product reaches more than 99.5%, and the selectivity of cyclohexanone oxime is improved.

[0021] 3. The present invention eliminates the use of a co-solvent while ensuring that the reaction efficiency does not decrease or even increases, thereby saving a large amount of energy consumption in the co-solvent separation link. The crude product obtained by the present invention has high purity and low energy consumption for subsequent refining. In addition, a residual ammonia recovery process is provided to almost completely convert all raw materials into butanone oxime and water, thereby achieving high raw material utilization and reduced material consumption. In addition, due to the high selectivity of the present invention for the main product, the content of by-products in the aqueous phase is extremely small, and the impurity content in the wastewater after the residual ammonia recovery is low, so the wastewater can be directly used as industrial water or irrigation water, thereby reducing energy consumption and material consumption.

[0022] 4. The present invention adopts a design of coating the catalyst with a fixed filler. Under the action of the high-speed centrifugal force provided by the rotating filler, the diffusion in the catalyst pores is enhanced, reducing the accumulation and blockage of reactants; the high selectivity of the present invention reduces the production of large molecular by-products and reduces the carbon accumulation on the catalyst surface. In summary, the present invention can increase the service life of the catalyst by 1 times compared with the current mainstream powder catalyst process, solves the problem of catalyst loss, and increases the service life of the catalyst.

[0023] 5. The present invention can achieve extremely high selectivity, the amount of hydrogen peroxide decomposition is extremely small, and the reaction of hydrogen peroxide directly oxidizing ammonia water to nitrogen oxides is also difficult to occur. Therefore, the content of oxygen and nitrogen oxides in the system is low. The reactor of the present invention is provided with an external circulation forced heat exchange, so that the heat energy of the oximation reaction can be quickly removed, and the mixing and flow in the reactor are sufficient and uniform, reducing the possibility of heat accumulation; in summary, the present invention optimizes the intrinsic safety of the cyclohexanone oxime production process, and the intrinsic safety of the production process is optimized. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 is a cross-sectional view of the reaction kettle in the present invention;

[0025] Figure 2 is a system flow chart of the present invention;

[0026] Figure 3 Schematic diagram of the reaction of cyclohexanone, ammonia and hydrogen peroxide under the catalysis of titanium silicalite TS-1.

[0027] In the figure: 1, hydrogen peroxide inlet; 2, cyclohexanone inlet; 3, ammonia water inlet; 4, hot steam inlet; 5, wastewater outlet; 6, reactor; 6-1, liquid feed inlet 1; 6-2, liquid feed inlet 2; 6-3, liquid feed inlet 3; 6-4, liquid distributor; 6-5, rotating filler; 6-6, rotating shaft; 6-7-bottom baffle; 6-8, sealing component; 6-9, jacket; 6-10, bottom liquid outlet; 6-11, motor; 6-12, external heat exchanger A; 6-13, external circulation pump A; 6-14, external heat exchanger B; 6-15, external circulation pump B; 7, phase separation tank; 8, water phase circulation pump; 9, evaporation tank; 10, cyclohexanone oxime outlet. DETAILED DESCRIPTION

[0028] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0029] Please refer to Figure 1-2, a device for continuously producing cyclohexanone oxime includes a reactor 6, which is composed of a liquid distributor 6-4, a rotating filler 6-5, a rotating shaft 6-6, a jacket 6-9, a bottom liquid outlet 6-10, an external heat exchanger A6-12, an external circulation pump A6-13, an external heat exchanger B6-14 and an external circulation pump B6-15. The top of the liquid distributor 6-4 is connected to a liquid feed port 1 6-1, a liquid feed port 2 6-2 and a liquid feed port 3 6-3, respectively. The bottom end of the liquid distributor 6-4 extends into the cavity of the rotating filler 6-5. The rotating filler 6-5 is fixed on the rotating shaft 6-6. A bottom baffle 6-7 is fixed on the surface of the rotating shaft 6-6 and located below the rotating filler 6-5. A sealing component 6-8 is fixed at the bottom, and the bottom end of the rotating shaft 6-6 is fixed to the sealing component 6-8. A motor 6-11 is fixed below the reactor 6, and the output shaft of the motor 6-11 is fixedly connected to the sealing component 6-8. External circulation pipelines are fixed on the left and right sides of the outside of the reactor 6, and the external circulation pipeline passes through the bottom of the reactor and is connected to the liquid distributor 6-4 after passing through an external circulation pump and an external heat exchanger. The rotating filler 6-5 is composed of any one of stainless steel embossed mesh filler, stainless steel wire mesh woven filler, alumina ceramic corrugated regular filler, plastic wire mesh filler, integral silicon carbide filler or foam metal filler, preferably stainless steel wire mesh filler and alumina ceramic corrugated regular filler, and the selected rotating filler 6-5 is coated with a titanium silicon molecular sieve film or other catalyst film.

[0030] A semi-enclosed shell is fixed to the outside of the rotating filler 6-5, and a series of spoiler components are fixed to the outside of the semi-enclosed shell to achieve better stirring effect. The bottom baffle is connected to the rotating shaft through a speed-changing gear set to achieve speed regulation.

[0031] A system for continuously producing cyclohexanone oxime comprises a hydrogen peroxide inlet 1, a cyclohexanone inlet 2, an ammonia water inlet 3, a hot steam inlet 4, a wastewater outlet 5, a reactor 6, a phase separation tank 7, a water phase circulation pump 8, an evaporation tank 9 and a cyclohexanone oxime outlet 10. The hydrogen peroxide inlet 1, the cyclohexanone inlet 2 and the ammonia water inlet 3 are respectively connected to a liquid feed inlet 1 6-1, a liquid feed inlet 2 6-2 and a liquid feed inlet 3 6-3. A bottom liquid outlet 6-10 is connected to a liquid inlet of the phase separation tank 7. A heavy phase outlet at the bottom of the phase separation tank 7 is connected to the cyclohexanone oxime outlet 10. A light phase outlet in the middle and upper part of the phase separation tank 7 is connected to the water phase circulation pump 8. The water phase circulation pump 8 is connected to the liquid inlet of the evaporation tank 9. A hot steam inlet 4 is connected to a gas inlet at the bottom of the evaporation tank 9. A liquid outlet at the bottom of the evaporation tank 9 is connected to a wastewater outlet. A liquid outlet at the top of the phase separation tank 7 is connected to a pipeline of the ammonia water inlet 3. A filler or a sieve plate structure is arranged in the evaporation tank 9.

[0032] A method for continuously producing cyclohexanone oxime, the method comprising the following steps:

[0033] Step 1: Freshly fed hydrogen peroxide liquid, cyclohexanone liquid and ammonia water are premixed in the liquid distributor 6-4 and then sprayed onto the rotating filler 6-5 at high speed. Oximation reaction occurs under the action of the catalyst loaded on the rotating filler 6-5. The reaction liquid sheared by the filler flows toward the wall of the reactor 6 under the joint action of the semi-enclosed shell and the bottom baffle 6-7. The rotation of the baffle and the spoiler of the filler shell lift the liquid upward and flow through the filler again to continue the reaction. The liquid level in the reactor is controlled above the filler. The amount ratio of ammonia water, hydrogen peroxide and cyclohexanone entering the liquid distributor is 1.1:1:1 to 1.5:1:1, and the optimal amount is 1.2:1:1. The pressure in the reactor is 1 to 10 atm, the liquid temperature is controlled at 45 to 150°C, preferably at 92 to 99°C at normal pressure, the residence time in the reactor is 30 to 200 min, preferably 65 to 85 min, and the rotation speed of the rotating packing is between 600 and 2500 rpm, preferably 1000 to 1500 rpm.

[0034] Step 2: Part of the reaction liquid in the kettle flows into the liquid distributor through an external circulation pump and an external heat exchanger, and is sprayed onto the rotating filler 6-5 through the liquid distributor 6-4 together with the freshly fed material. The external heat exchanger and the reactor jacket jointly remove the reaction heat. The material after sufficient reaction in the reactor 6 is extracted from the bottom of the reactor 6 and enters the phase separation tank. The crude cyclohexanone oxime product is extracted from the heavy phase and sent to the cyclohexanone oxime refining section, and the ammonia-containing wastewater is extracted from the light phase;

[0035] Step 3: The ammonia-containing wastewater is countercurrently contacted with hot steam in the evaporation tank 9, and the ammonia is fully stripped by the water vapor and dissolved into the freshly fed concentrated ammonia water; the wastewater after evaporation of the residual ammonia is sent to the wastewater treatment unit.

[0036] Example 1

[0037] The system, device and method of the present invention are used to continuously react and prepare cyclohexanone oxime, using TS-1 catalyst. The molar flow rate of the cyclohexanone feed is 1, and the ratio (r) of the molar flow rate of ammonia water and hydrogen peroxide entering the liquid distributor is 1.2:1.01; the pressure in the reactor is 1atm, and the liquid temperature (T) is controlled at 95°C; the residence time (t) of the material in the reactor is 70 minutes, and the speed (N) of the rotating filler is 1000rpm. After stable operation for 4 hours, the concentration of each outlet substance is measured, and the selectivity of cyclohexanone oxime in the product is calculated to be (a) 99.6%, the cyclohexanone conversion rate (b) is 100%, the ammonia conversion rate (c) is 98.1%, and the hydrogen peroxide conversion rate (d) is 99.2%.

[0038] Embodiment 2-10

[0039] The implementation method is the same as that of Example 1, except that the operating parameters are changed. For the sake of simplicity, the parameters and their units appearing in Example 1 are expressed with marked letters.

[0040]

[0041] Among them, Examples 1 to 4 are within the process parameter range claimed by the present invention. From the results of the examples, it can be concluded that the present invention can significantly improve the conversion rate of raw materials and the selectivity of products.

[0042] Among them, some process operation parameters of Examples 5 to 10 are outside the process parameter range claimed by the present invention, which are comparative examples. The comparative examples can reversely prove that the effect achieved by the process of the present invention is indeed obtained by the relative process and equipment improvements made by the present invention.

[0043] It should be noted that, in this article, relational terms such as first and second, etc. are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Moreover, the terms "include", "comprise" or any other variants thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, the elements defined by the sentence "comprise a ..." do not exclude the existence of other identical elements in the process, method, article or device including the elements.

[0044] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A system for continuously producing cyclohexanone oxime, comprising a hydrogen peroxide inlet (1), a cyclohexanone inlet (2), an ammonia water inlet (3), a hot steam inlet (4), a wastewater outlet (5), a reaction kettle (6), a phase separation tank (7), a water phase circulation pump (8), an evaporation tank (9) and a cyclohexanone oxime outlet (10), Features: The reactor (6) is composed of a liquid distributor (6-4), a rotating filler (6-5), a rotating shaft (6-6), a jacket (6-9), a bottom liquid outlet (6-10), an external heat exchanger A (6-12), an external circulation pump A (6-13), an external heat exchanger B (6-14) and an external circulation pump B (6-15). The top of the liquid distributor (6-4) is connected to a liquid feed port 1 (6-1), a liquid feed port 2 (6-2) and a liquid feed port 3 (6-4). Inlet three (6-3), the bottom end of the liquid distributor (6-4) extends into the cavity of the rotating filler (6-5), the rotating filler (6-5) is fixed on the rotating shaft (6-6), a bottom baffle (6-7) is fixed on the surface of the rotating shaft (6-6) and below the rotating filler (6-5), a sealing component (6-8) is fixed at the bottom of the reactor (6), the bottom end of the rotating shaft (6-6) is fixed to the sealing component (6-8), and the bottom of the reactor (6) A motor (6-11) is fixedly arranged, and an output shaft of the motor (6-11) is fixedly connected to a sealing component (6-8). External circulation pipelines are fixedly arranged on both left and right sides of the outside of the reactor (6). The hydrogen peroxide inlet (1), the cyclohexanone inlet (2) and the ammonia water inlet (3) are respectively connected to the liquid feed inlet 1 (6-1), the liquid feed inlet 2 (6-2) and the liquid feed inlet 3 (6-3). The bottom liquid outlet (6-10) is connected to the liquid inlet of the phase separation tank (7). The heavy phase outlet at the bottom of the phase separation tank (7) is connected to the cyclohexanone oxime outlet (10), the light phase outlet at the middle and upper part of the phase separation tank (7) is connected to the water phase circulation pump (8), the water phase circulation pump (8) is connected to the liquid inlet of the evaporation tank (9), the hot steam inlet (4) is connected to the gas inlet at the bottom of the evaporation tank (9), the liquid outlet at the bottom of the evaporation tank (9) is connected to the wastewater outlet, and the liquid outlet at the top of the phase separation tank (7) is connected to the pipeline of the ammonia water inlet (3).

2. A system for continuous production of cyclohexanone oxime according to claim 1, Features: A filler or a sieve plate structure is arranged inside the evaporation tank (9).

3. A system for continuous production of cyclohexanone oxime according to claim 1, Features: The rotating filler (6-5) is any one of stainless steel crimped mesh filler, stainless steel wire mesh woven filler, alumina ceramic corrugated regular filler, plastic wire mesh filler, integral silicon carbide filler or foam metal filler, and the selected rotating filler (6-5) is coated with a titanium silicon molecular sieve film or other catalyst film.

4. A system for continuous production of cyclohexanone oxime according to claim 1, Features: A semi-enclosed shell is fixed to the outside of the rotating filler (6-5), and a series of spoiler components are fixed to the outside of the semi-enclosed shell. The bottom baffle is connected to the rotating shaft via a speed change gear set.

5. A method for continuously producing cyclohexanone oxime, using the system for continuously producing cyclohexanone oxime according to claim 1, It is characterized in that The production method comprises the following steps: Step 1: freshly fed hydrogen peroxide liquid, cyclohexanone liquid and ammonia water are premixed in a liquid distributor (6-4) and then sprayed onto a rotating filler (6-5) at high speed. An oximation reaction occurs under the action of a catalyst loaded on the rotating filler (6-5). The reaction liquid sheared by the filler flows toward the wall of the reactor (6) under the combined action of a semi-enclosed shell and a bottom baffle (6-7). The rotation of the baffle and the spoiler of the filler shell lift the liquid upward and flow through the filler again to continue the reaction. The liquid level in the reactor is controlled above the filler. The molar ratio of ammonia water, hydrogen peroxide and cyclohexanone entering the liquid distributor is 1.1:1:1 to 1.5:1:

1. Step 2: Part of the reaction liquid in the reactor flows into the liquid distributor through an external circulation pump and an external heat exchanger, and is sprayed onto the rotating filler (6-5) through the liquid distributor (6-4) together with the freshly fed material. The external heat exchanger and the reactor jacket jointly remove the reaction heat. The material after sufficient reaction in the reactor (6) is taken out from the bottom of the reactor (6) and enters the phase separation tank (7). The crude cyclohexanone oxime product is taken out from the heavy phase and sent to the cyclohexanone oxime refining section, and the ammonia-containing wastewater is taken out from the light phase; Step 3: The ammonia-containing wastewater is countercurrently contacted with hot steam in the evaporation tank (9), and the ammonia gas is fully stripped by the water vapor and dissolved into the freshly fed concentrated ammonia water; the wastewater after evaporation of the residual ammonia is sent to the wastewater treatment unit.

6. A method for continuously producing cyclohexanone oxime according to claim 5, Features: In the step 1, the pressure in the reactor is 1-10 atm, the liquid temperature is controlled at 45-150° C., the residence time in the reactor is 30-200 min, and the rotation speed of the rotating filler is between 600-2500 rpm.

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