CN112827462A

CN112827462A - Loop reactor for preparing p-nitrophenyl ether and preparation method of p-nitrophenyl ether

Info

Publication number: CN112827462A
Application number: CN202110243744.6A
Authority: CN
Inventors: 梅华; 朱林
Original assignee: JIANGSU NUOMENG CHEMICAL CO Ltd
Current assignee: JIANGSU NUOMENG CHEMICAL CO Ltd
Priority date: 2021-03-05
Filing date: 2021-03-05
Publication date: 2021-05-25

Abstract

The invention discloses a loop reactor for preparing p-nitrophenyl ether, which comprises a reaction kettle, a circulating pump, a heat exchanger and a Venturi ejector, wherein the circulating pump is arranged in the reaction kettle; venturi ejector inducer opening inside diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (1.5-4): (2-6): (90-260): (800-1800); the opening angle of the diffuser section is 8-28 degrees. The invention adopts the loop reactor to prepare the paranitroacetophenone, and compared with the traditional kettle type reactor, the preparation method does not need to adopt a phase transfer catalyst, thereby avoiding the subsequent recovery treatment step. Meanwhile, the process gas introduced into the gas inlet of the loop reactor is regulated and controlled, the mutual diffusion between gas and liquid is promoted through the gas via the Venturi ejector, the mass transfer process between liquid-liquid heterogeneous reaction materials is enhanced, and the reaction time is effectively shortened.

Description

Loop reactor for preparing p-nitrophenyl ether and preparation method of p-nitrophenyl ether

Technical Field

The invention belongs to the technical field of chemical production, and particularly relates to a method for synthesizing paranitroacetophenone by adopting novel reactor equipment, namely a loop reactor.

Background

P-nitrophenyl ether is an important fine organic intermediate. The p-aminophenylethyl ether can be prepared by hydrogenation, and can be widely used for preparing dyes, analgesic drugs, rubber anti-aging agents, food antioxidants and other fields. At present, para-nitrochlorobenzene, ethanol and sodium hydroxide are mainly used as raw materials for etherification reaction in industrial production. The p-nitrochlorobenzene and the sodium hydroxide/ethanol/water solution are not mutually soluble to cause layering, the reaction is carried out at the temperature higher than 70 ℃ under the action of a phase transfer catalyst, the reaction time generally exceeds 6 hours, and the production efficiency is low. A phase transfer catalyst is adopted in the synthesis process, so that the problems of subsequent separation and product purity are caused; p-nitrochlorobenzene generates p-nitrophenolate and azo byproducts in the reaction process, and the product yield is reduced. In addition, the reaction is exothermic, and sodium hydroxide needs to be fed in batches in the production process to avoid increasing side reactions due to too high temperature rise.

The loop reactor is a novel reactor system and particularly comprises a reaction kettle, a circulating pump, a heat exchanger and a Venturi ejector (mixer). The reaction liquid circulates in a loop at a large flow rate, is injected at a high speed through a Venturi ejector (mixer), and forms negative pressure at a working nozzle, so that the process gas is sucked into the ejector to form micron-sized bubbles with large specific surface area, the gas-liquid contact is increased, and the gas-liquid (or gas-liquid-solid) multiphase reaction speed is accelerated. Bubbles in the loop reactor divide and shear liquid in a jet mixing area and liquid in the reaction kettle, promote diffusion mass transfer between heterogeneous liquid, and play a role in strong stirring, so that the liquid-liquid heterogeneous reaction speed is increased, and the reaction conversion rate and the product selectivity are further influenced.

Loop reactors are currently used primarily in heterogeneous reaction processes where gases participate in chemical reactions. The venturi ejector (mixer) is an important device in the whole reaction system, and the specific design specification parameters of the venturi ejector (mixer) are at least based on the following factors: material density, surface tension, viscosity, gas-liquid dissolution rate under process temperature and pressure. The liquid flow rate and the gas type are also key factors for improving the gas-liquid or gas-liquid-solid heterogeneous reaction speed. For a liquid-liquid heterogeneous production process in which gas does not participate in chemical reaction, the mass transfer process between liquid reactants is enhanced by changing the design size of a venturi ejector (mixer), and the method is rarely reported.

Disclosure of Invention

The invention aims to overcome the defects in the prior art and provide a method for synthesizing p-nitrophenyl ethyl ether, which can effectively shorten the reaction time and improve the reaction yield.

In order to achieve the above object, the present invention provides a loop reactor for preparing p-nitrophenyl ether, comprising a reaction kettle, a circulation pump, a heat exchanger and a venturi ejector; the bottom of the reaction kettle is communicated with a heat exchanger through a circulating pump; the heat exchanger is communicated with a Venturi ejector arranged at the top end of the reaction kettle; the Venturi ejector comprises an inlet section, a nozzle, a mixing section and a diffusion section which are communicated in sequence; the inlet section and the nozzle are in a tapered tubular shape; the periphery of the inlet section and the nozzle is provided with a tapered annular air chamber which is communicated with the mixing section; the diffusion section is a gradually expanding pipe type; an air inlet is arranged on one side of the top of the reaction kettle; the outer side of the gas chamber is provided with a gas circulating pipe, and the gas chamber is communicated with a gas inlet of the reaction kettle through the gas circulating pipe; venturi ejector inducer opening inside diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (1.5-4): (2-6): (90-260): (800-1800); the opening angle of the diffuser section is 8-28 degrees.

The invention takes the loop reactor as a reaction container, and introduces process gas which does not participate in the reaction to adjust the reaction pressure so as to promote the mass transfer process among the original reaction materials (the p-nitrochlorobenzene, the sodium hydroxide and the ethanol), and simultaneously improves and designs the Venturi ejector so that the venturi ejector is more suitable for preparing the p-nitrophenetole, obtains better yield and effectively shortens the reaction time.

In some embodiments, it is preferable that the venturi injector has an inner diameter of the inlet section opening: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (1.5-4): (2-6): (110-260): (1100-1800); the opening angle of the diffuser section is 12-28 degrees.

The design of the loop reactor is more suitable for introducing hydrogen as process gas, and has more effective reaction promoting effect on the preparation of paranitroanisole.

In some embodiments, it is preferable that the venturi injector has an inner diameter of the inlet section opening: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (2-3.5): (3-5): (140-220): (1400-1600); the opening angle of the diffusion section is 15-25 degrees.

In some embodiments, it is more preferable that the venturi injector has an inner diameter of the inducer opening: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: 3: 4: 200: 1400; the opening angle of the diffuser section is 20 °.

In some embodiments, it is preferable that the ratio of the height to the diameter of the reaction kettle is (6-8): 1.

the invention also provides a preparation method of the p-nitrophenyl ether by using the loop reactor, wherein the preparation method takes p-nitrochlorobenzene, sodium hydroxide and ethanol as raw materials to carry out etherification reaction to prepare the p-nitrophenyl ether; the method comprises the steps of preparing p-nitrophenyl ether by adopting the loop reactor, placing raw materials in a reaction kettle of the loop reactor before etherification reaction begins, introducing process gas (namely gas which does not participate in the p-nitrophenyl ether preparation reaction) into the loop reactor through a gas inlet of the reaction kettle to reaction pressure in the etherification reaction process, and controlling the linear velocity of fluid at a nozzle of a Venturi ejector to be 90-130 m/s.

The invention promotes the mutual diffusion among all phases by introducing the process gas under the condition of adding the gas, strengthens the mass transfer process among the original reaction materials (the p-nitrochlorobenzene, the sodium hydroxide and the ethanol), and effectively shortens the reaction time.

The process gas adopts hydrogen or nitrogen.

When hydrogen is used as the process gas, in some embodiments, the reaction pressure is preferably 0.4 to 1.3 MPa. When hydrogen is introduced as the process gas, the reaction pressure is controlled, and the reaction is further optimized.

In some embodiments, it is preferred that the mass ratio of p-nitrochlorobenzene, sodium hydroxide and ethanol is 1: (1.2-2.1): (2-3); and in the etherification reaction process, controlling the reaction temperature to be 55-65 ℃; the reaction time is 40-80 min.

In some embodiments, the reaction pressure is preferably 0.5-1.1 MPa, and the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 105-120 m/s.

In some embodiments, it is preferred that the mass ratio of p-nitrochlorobenzene, sodium hydroxide and ethanol is 1: 1.7: 2.5; in the etherification reaction process, the reaction pressure is controlled to be 0.8MPa, the reaction temperature is controlled to be 60 ℃, the reaction time is 50min, and the linear velocity of fluid at the nozzle of the Venturi ejector is controlled to be 113 m/s.

Compared with the prior art, the invention has the following advantages:

1. the invention adopts the loop reactor to prepare the paranitroacetophenone, and compared with the traditional kettle type reactor, the preparation method does not need to adopt a phase transfer catalyst, thereby avoiding the subsequent recovery treatment step. Meanwhile, the process gas introduced into the gas inlet of the loop reactor is regulated and controlled, the mutual diffusion between gas and liquid is promoted through the gas via the Venturi ejector, the mass transfer process between liquid-liquid heterogeneous reaction materials is enhanced, and the reaction time is effectively shortened.

2. The preparation method of paranitroacetophenone optimizes the reaction effect by controlling key process parameters, namely specification and size of the Venturi ejector and linear velocity of fluid at the nozzle of the Venturi ejector in the reaction process.

3. The invention explores the influence of relevant process parameters such as pressure, temperature and the like of a reaction system on the reaction when different process gases are introduced, seeks the optimal corresponding process parameters in the reaction process and realizes the optimization of the reaction effect.

4. The preparation method can improve the selectivity, reduce the generation rate of byproducts, improve the product yield, avoid the operation problem of batch feeding in actual production, effectively save the cost and realize green and energy conservation.

Drawings

FIG. 1 is a schematic structural diagram of a loop reactor for preparing p-nitrophenyl ether according to the invention;

FIG. 2 is a schematic structural view of the venturi ejector of FIG. 1;

in the figure, 1-reaction kettle, 2-Venturi ejector, 3-heat exchanger, 4-circulating pump, 5-gas circulating pipe, 6-inlet section, 7-mixing section, 8-diffusion section, 9-nozzle and 10-gas chamber.

Detailed Description

The invention is described in detail below with reference to the figures and the specific embodiments.

As shown in figure 1, the invention adopts a loop reactor to carry out batch reaction to prepare the paranitroanisole. The loop reactor comprises a reaction kettle 1, a circulating pump 4, a heat exchanger 3 and a Venturi ejector 2.

When the reactor works, the circulating pump is started. The reaction liquid circulates in the loop at a high flow rate, the venturi ejector 2 ejects at a high speed, and a negative pressure is formed at the working nozzle, so that gas (process gas) is sucked into the venturi ejector. One side of the top of the reaction kettle 1 is provided with a branch pipe which is connected with an air inlet and can form air circuit circulation locally. The micro bubbles with large specific surface area are formed in the Venturi ejector, mutual diffusion between gas and liquid is promoted through the gas in the Venturi ejector, the mass transfer process between liquid and liquid heterogeneous reaction materials is strengthened, and the reaction time is effectively shortened. . The lower end of the Venturi ejector is positioned below the liquid level, and the gas-liquid mixed material and the materials in the reaction kettle are impacted, so that the effect of promoting dispersion and mixing is achieved, and the reaction is promoted to further proceed. The material enters the heat exchanger from the bottom end of the reaction kettle through the circulating pump 4 and enters the Venturi ejector 2 from the top end of the reaction kettle 1. The heat exchanger 3 removes or provides heat released or absorbed in the reaction process, and controls the fluctuation of the reaction temperature to +/-1 ℃. And (3) gradually reducing the reactants and gradually increasing the products along with the reaction, and discharging the products from the bottom end of the reaction kettle after the reaction is completely finished.

The heat exchanger in this patent can adopt tubular heat exchanger or plate heat exchanger.

Aiming at a specific certain chemical reaction process under a certain pressure and temperature condition, the design structure size of the Venturi ejector greatly influences the effect of mutual dispersion and contact between reaction substances, thereby finally influencing the chemical production efficiency. With reference to fig. 2, the venturi ejector of the present patent is composed in particular of an inlet section 6 in the shape of a convergent tube, a mixing section 7, a diffuser section 8, a nozzle 9 and a gas chamber 10. As shown in FIG. 1, a gas circulation pipe 5 is provided on the side of the gas chamber 1 and connected to the top gas inlet of the reaction vessel 1 to provide a gas circulation space in a local region.

Reaction operation: dissolving sodium hydroxide in ethanol, and controlling the molar ratio of NaOH to ethanol; at room temperature, adding sodium hydroxide/ethanol solution and p-nitrochlorobenzene into a reaction kettle of a loop reactor through a feed inlet. Introducing process gas into the reactor through a gas inlet until the system pressure is 2MPa, starting a circulating pump 4 to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, maintaining a certain pressure of the reaction system, heating to the reaction temperature (the heating time is about 10min), immediately supplementing the process gas to the reaction pressure, and adjusting the circulating pump 4 until the flow rate reaches a certain value, and recording as the reaction starting time.

When the reaction is finished, the flow rate of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min). And (4) emptying the gas in the kettle and discharging the liquid in the kettle (the liquid obtained at the moment is a mixed solution). Adding hydrochloric acid into the mixed solution discharged from the reaction kettle, oscillating until the pH value is 7, standing for layering, taking an oil layer, performing gas chromatography analysis on the oil layer to obtain the composition, and performing reduced pressure distillation to calculate the actual yield according to the quality of the p-nitrophenyl ether product obtained by final distillation and the quality of the p-nitrochlorobenzene in the reaction raw materials.

GC analysis conditions were as follows: the method comprises the following steps of performing area normalization treatment to calculate the content of paranitroanisole in a reaction product, wherein the gas chromatograph of Nanjing Kejie GC-5890 type is a SE54-30M capillary column, the temperature of a gasification chamber is 250 ℃, the temperature of a FID detector is 300 ℃, the temperature of a column box is increased by program, the temperature is increased to 260 ℃ from 100 ℃ at a speed of 10 ℃/min.

Example 1 (Hydrogen gas for Process gas)

1458g of p-nitrochlorobenzene, 1156g of 50 wt% aqueous NaOH solution and 978g of ethanol are sequentially added into a 5L loop reactor (reactor volume 5L) shown in FIG. 1 through feeding ports, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol is 1: 1.7: 2.5. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.3MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 0.8MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after 50min of reaction, the flow rate of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 113m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 200: 1400. the diffuser opening angle α is 20 °, as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 97.3%. The actual yield of the product was 97% calculated by distillation under reduced pressure.

Example 2 (Hydrogen gas for Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1630g of p-nitrochlorobenzene, 1064g of a 50 wt% aqueous NaOH solution, 962g of ethanol through feed ports, and a total volume of about 3240ml, wherein the molar ratio of p-nitrochlorobenzene to NaOH to ethanol was 1: 1.4: 2.2. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.2MPa, heating to the reaction temperature (the heating time is about 10min) of 63 ℃, immediately supplementing hydrogen to the reaction pressure of 0.5MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 70min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

In the reaction process, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 123m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 2: 3: 140:1500, diffuser opening angle α is 25 °, as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 93.7%. The actual yield of the product was 92.1% as calculated by distillation under reduced pressure.

Example 3 (Hydrogen gas for Process gas)

1544g of p-nitrochlorobenzene, 936g of a 50 wt% aqueous NaOH solution and 1120g of ethanol are sequentially added to a 5L loop reactor (reactor volume 5L) shown in FIG. 1 through feed ports, and the total volume is about 3280ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol is 1: 1.3: 2.7. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.5MPa, heating to the reaction temperature (the heating time is about 10min) of 57 ℃, immediately supplementing hydrogen to the reaction pressure of 1.1MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 105m/s, and the detailed design dimension is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 2.5: 3.5: at 220:1600 deg., and a diffuser opening angle alpha of 15 deg., as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 90.4%. The actual yield of the product was 90% by distillation under reduced pressure.

Example 4 (Hydrogen gas for Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1372g of p-nitrochlorobenzene, 50 wt% aqueous NaOH 1216, and 1030g of ethanol through feed ports, to a total volume of about 3100ml, wherein the molar ratio of p-nitrochlorobenzene to NaOH to ethanol was 1: 1.6: 2.8. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.3MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 0.6MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

In the reaction process, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 97m/s, and the detailed design size is specifically that the inner diameter of an inlet section opening is D1: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 120:1200, diffuser opening angle alpha is 18 deg., as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 90.9%. The actual yield of the product was 89.4% as calculated by distillation under reduced pressure.

Example 5 (Hydrogen gas for Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1372g of p-nitrochlorobenzene, 1216g of a 50 wt% aqueous NaOH solution, and 1030g of ethanol through feed ports, to a total volume of about 3240ml, wherein the molar ratio of p-nitrochlorobenzene to NaOH to ethanol was 1: 1.9: 2.8. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.5MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 0.9MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 120m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3.5: 5: 160:1500, diffuser opening angle α is 15, as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 92.8%. The actual yield of the product was 90.5% as calculated by distillation under reduced pressure.

Example 6 (Hydrogen gas for Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1630g of p-nitrochlorobenzene, 1140g of a 50 wt% NaOH aqueous solution, 875g of ethanol through feed ports, and the total volume was about 3200ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.5: 2. introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.3MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 0.7MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 120m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 1700 with a diffuser opening angle alpha of 22 deg., as shown in figure 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 89.5%. The actual yield of the product was 87% by distillation under reduced pressure.

Example 7 (Nitrogen as Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1, 1715g of p-nitrochlorobenzene, 1200g of 50 wt% NaOH aqueous solution and 780g of ethanol were sequentially added through feed ports, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.5: 1.7. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, the pressure of the reaction system is kept at 1MPa, the temperature is raised to 60 ℃ at the reaction temperature (the temperature rise time is about 10min), and then N is supplemented immediately₂When the reaction pressure is 2MPa, the circulating pump is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after 50min of reaction, the flow rate of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 115m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 140: the diffuser section opening angle α is 14 ° as shown in fig. 2 at 1200.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 98.3%. The actual yield of the product was 98.9% as calculated by distillation under reduced pressure.

Example 8 (Nitrogen as Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1760g of p-nitrochlorobenzene, 1150g of 50 wt% aqueous NaOH solution, 770g of ethanol via feed ports, and a total volume of about 3160ml, wherein the molar ratio of p-nitrochlorobenzene to NaOH to ethanol was 1: 1.2: 1.4. is reversely rotated through the air inletIntroducing N into the reactor₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, the pressure of the reaction system is kept at 1MPa, the temperature is raised to 60 ℃ at the reaction temperature (the temperature rise time is about 10min), and then N is supplemented immediately₂When the reaction pressure is 1.7MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the start of the reaction is recorded. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 125m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 2: 3: 150: 1000 with the diffuser section opening angle alpha at 11 deg., as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 95.3%. The actual yield of the product was 94.5% as calculated by distillation under reduced pressure.

Example 9 (Nitrogen as Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1, 1610g of p-nitrochlorobenzene, 1144g of 50 wt% aqueous NaOH solution, and 810g of ethanol were sequentially fed via feed ports, and the total volume was about 3090ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.3: 1.6. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, the pressure of the reaction system is kept at 1MPa, the temperature is raised to 55 ℃ at the reaction temperature (the temperature rise time is about 10min), and then N is supplemented immediately₂When the reaction pressure is 2.1MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 70min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction process, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 100m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 2.5: 3.5: 140: the diffuser opening angle α is 15 ° as shown in fig. 2 1300.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 93.7%. The actual yield of the product was 92% calculated by distillation under reduced pressure.

Example 10 (Nitrogen as Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1 were sequentially fed 1464g of p-nitrochlorobenzene, 1280g of a 50 wt% aqueous NaOH solution, and 874g of ethanol via feed ports, wherein the molar ratio of p-nitrochlorobenzene to NaOH to ethanol was 1: 1.6: 1.9. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, the pressure of the reaction system is kept at 1MPa, the temperature is raised to 55 ℃ at the reaction temperature (the temperature rise time is about 10min), and then N is supplemented immediately₂When the reaction pressure is 2.3MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 105m/s, and the detailed design dimension is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 170: 1400, the diffuser section opening angle α is 18 ° as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 92.3%. The actual yield of the product was 93% by distillation under reduced pressure.

Example 11 (Nitrogen as Process gas)

To a 5L loop reactor (reactor volume 5L) shown in FIG. 1, 1320g of p-nitrochlorobenzene, 1080g of 50 wt% NaOH aqueous solution and 950g of ethanol were sequentially added through feed ports, and the total volume was about 3000ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.5: 2.3. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. After the last replacement, the pressure of the reaction system is kept at 1MPa, the temperature is raised to 60 ℃ at the reaction temperature (the temperature rise time is about 10min), and then N is supplemented immediately₂When the reaction pressure is 2MPa, the circulating pump 4 is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 120m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3.5: 5: 160: at 1500, the diffuser section opening angle α is 15, as shown in FIG. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 91.1%. The actual yield of the product was 92% calculated by distillation under reduced pressure.

Example 12 (Nitrogen as Process gas)

1025g of p-nitrochlorobenzene, 780g of a 50 wt% aqueous NaOH solution and 1350g of ethanol were sequentially added to a 5L loop reactor (5L reactor volume) shown in FIG. 1 through feed ports, and the total volume was about 3050ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.4: 2. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. Keeping the pressure of the reaction system at 1MPa after the last replacement, and heating to the reaction temperature55 ℃ at the temperature (the temperature rise time is about 10min), and N is supplemented immediately after the temperature rise time is up to 55 DEG C₂When the reaction pressure is 2.3MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

In the reaction process, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 123m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 105: 1100, the diffuser section opening angle alpha is 10 deg., as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 93.4%. The actual yield of the product was 92.5% as calculated by distillation under reduced pressure.

Comparative example 1

170g of p-nitrochlorobenzene, 78g of ethanol and 15g of phase transfer catalyst tetrabutylammonium bromide are added into a 500ml four-mouth bottle provided with an electric stirrer, a reflux condenser tube, a dropping funnel and a thermometer at one time, 120g of 50 wt% NaOH aqueous solution is slowly dropped under the condition of water bath at 60 ℃, and the dropping time is about 45 min. The molar ratio of the raw materials of the p-nitrochlorobenzene to the NaOH to the ethanol is specifically 1: 1.5: 1.7, total volume about 360 ml. After 8h of reaction, the water bath was removed and the stirring was stopped. Adding hydrochloric acid into the mixed solution, shaking until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 72.5%. The actual yield of the product was 69.8% as calculated by distillation under reduced pressure.

As can be seen from comparative example 1, when the reaction kettle is used for preparing the paranitroacetophenone, the yield and the content are obviously lower than those obtained by using a loop reactor, and the reaction time is long.

Comparative example 2

1458g of p-nitrochlorobenzene, 1156g of 50 wt% aqueous NaOH solution and 978g of ethanol are sequentially added into a 5L loop reactor (reactor volume 5L) shown in FIG. 1 through feeding ports, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol is 1: 1.7: 2.5. . Introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 1.5MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 2.0MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after 50min of reaction, the flow rate of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 85.3%. The actual yield of the product was 83.5% as calculated by distillation under reduced pressure.

As can be seen from comparative example 2, when hydrogen was used as the process gas, the p-nitrophenyl ether content in the product and the yield of the reaction were significantly reduced when the reaction pressure was increased to some extent.

Comparative example 3

1458g of p-nitrochlorobenzene, 1156g of 50 wt% aqueous NaOH solution and 978g of ethanol are sequentially added into a 5L loop reactor (reactor volume 5L) shown in FIG. 1 through feeding ports, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol is 1: 1.7: 2.5. . Introducing hydrogen into the reactor through the air inlet until the system pressure is 2MPa, starting a circulating pump to enable liquid in the reactor to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. And (3) after the last replacement, keeping the pressure of the reaction system at 0.3MPa, heating to the reaction temperature (the heating time is about 10min) of 60 ℃, immediately supplementing hydrogen to the reaction pressure of 0.8MPa, adjusting a circulating pump until the flow rate reaches a certain value, and recording as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 60min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

During the reaction, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 113m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 70:1400 and a diffuser opening angle alpha of 20 deg., as shown in fig. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 78.4%. The actual yield of the product was 76% as calculated by distillation under reduced pressure.

As can be seen from comparative example 3, when hydrogen was used as the process gas, the p-nitrophenyl ether content in the product and the yield of the reaction were significantly reduced when the length of the mixing section in the Venturi ejector was reduced to a certain extent.

Comparative example 4

1025g of p-nitrochlorobenzene, 780g of a 50 wt% aqueous NaOH solution and 1350g of ethanol were sequentially added to a 5L loop reactor (5L reactor volume) shown in FIG. 1 through feed ports, and the total volume was about 3050ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.4: 2. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. Maintaining the pressure of the reaction system at 0.7MPa after the last replacement, heating to 55 ℃ at the reaction temperature (the heating time is about 10min), and immediately supplementing N₂When the reaction pressure is 1.1MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the start of the reaction is recorded. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 90min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 84.3%. The actual yield of the product was 82% calculated by distillation under reduced pressure.

As can be seen from comparative example 4, when nitrogen was used as the process gas, the content of paranitroanisole in the product and the yield of the reaction were significantly reduced when the reaction pressure was reduced to a certain extent.

Comparative example 5

1025g of p-nitrochlorobenzene, 780g of a 50 wt% aqueous NaOH solution and 1350g of ethanol were sequentially added to a 5L loop reactor (5L reactor volume) shown in FIG. 1 through feed ports, and the total volume was about 3050ml, wherein the molar ratio of the p-nitrochlorobenzene to the NaOH to the ethanol was 1: 1.4: 2. introducing N into the reactor through an air inlet₂When the system pressure is 2MPa, starting a circulating pump to enable the liquid in the kettle to slowly flow, emptying the gas, and repeatedly replacing the air in the loop reactor for 6 times. Maintaining the pressure of the reaction system at 0.7MPa after the last replacement, heating to 55 ℃ at the reaction temperature (the heating time is about 10min), and immediately supplementing N₂When the reaction pressure is 2.3MPa, the circulation pump 4 is adjusted until the flow rate reaches a certain value, and the reaction is recorded as the beginning of the reaction. The reaction temperature and the reaction pressure are maintained, and after the reaction is carried out for 90min, the flow speed of the circulating pump 4 is immediately reduced and the temperature is rapidly reduced to the room temperature (the temperature reduction time is about 10 min).

In the reaction process, the linear velocity of the fluid at the nozzle of the Venturi ejector is controlled to be 123m/s, and the detailed design size is specifically that the inner diameter D1 of the opening of the inlet section: nozzle inner diameter D2: air chamber closing-in inner diameter D3: mixing segment length L1: the ratio of diffuser length L2 is 38: 3: 4: 40: at 850, the diffuser section opening angle α is 10, as shown in FIG. 2.

Adding hydrochloric acid into the mixed solution obtained after the reaction is finished, oscillating until the pH value is 7, standing for layering, taking an oil layer, and performing gas chromatography analysis on the oil layer to obtain an oily product with the p-nitrophenyl ethyl ether content of 76.4%. The actual yield of the product was 74.1% as calculated by distillation under reduced pressure.

As can be seen from comparative example 5, when nitrogen was used as the process gas, the p-nitrophenyl ether content in the product and the yield of the reaction were significantly reduced when the length of the mixing section in the Venturi ejector was reduced to a certain extent.

Claims

1. A loop reactor for preparing p-nitrophenyl ether, characterized in that it comprises a reaction kettle, a circulation pump, a heat exchanger and a Venturi ejector; the bottom of the reaction kettle is communicated with the heat exchanger through the circulating pump; the heat exchanger is communicated with the Venturi ejector arranged at the top end of the reaction kettle; the Venturi ejector comprises an inlet section, a nozzle, a mixing section and a diffusion section which are communicated in sequence; the inlet section and the nozzle are in a tapered tubular shape; the periphery of the inlet section and the nozzle is provided with a tapered annular air chamber which is communicated with the mixing section; the diffusion section is of a gradually expanding pipe type; an air inlet is formed in one side of the top of the reaction kettle; a gas circulating pipe is arranged on the outer side of the gas chamber, and the gas chamber is communicated with a gas inlet of the reaction kettle through the gas circulating pipe; the venturi ejector has an inlet section opening inner diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (1.5-4): (2-6): (90-260): (800-1800); the opening angle of the diffusion section is 8-28 degrees.

2. The loop reactor of claim 1 wherein the venturi injector has an inducer opening inside diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (1.5-4): (2-6): (110-260): (1100-1800); the opening angle of the diffusion section is 12-28 degrees.

3. The loop reactor of claim 2 wherein the venturi injector has an inducer opening internal diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: (2-3.5): (3-5): (140-220): (1400-1600); the opening angle of the diffusion section is 15-25 degrees.

4. The loop reactor of claim 3 wherein the venturi injector has an inducer opening inside diameter: nozzle bore diameter: the inner diameter of the closed air chamber: length of mixed section: the ratio of the length of the diffusion section is 38: 3: 4: 200: 1400; the opening angle of the diffuser section is 20 °.

5. The loop reactor of claim 2, wherein the ratio of the height to the diameter of the reaction kettle is (6-8): 1.

6. the preparation method of the paranitroacetophenone by adopting the loop reactor of any one of claims 1 to 5, wherein the paranitroacetophenone is prepared by carrying out etherification reaction on paranitrochlorobenzene, sodium hydroxide and ethanol which are used as raw materials; the method is characterized in that the paranitroacetophenone is prepared by adopting the loop reactor, before the etherification reaction starts, raw materials are placed in a reaction kettle of the loop reactor, in the etherification reaction process, process gas is introduced into the loop reactor through a gas inlet of the reaction kettle to reaction pressure, and the linear velocity of fluid at a nozzle of a Venturi ejector is controlled to be 90-130 m/s.

7. The method according to claim 6, wherein the process gas is hydrogen or nitrogen.

8. The preparation method according to claim 7, wherein when hydrogen is used as the process gas, the reaction pressure is 0.4 to 1.3 MPa; the mass ratio of the p-nitrochlorobenzene to the sodium hydroxide to the ethanol is 1: (1.2-2.1): (2-3); in the etherification reaction process, the reaction temperature is controlled to be 55-65 ℃; the reaction time is 40-80 min.

9. The preparation method according to claim 8, wherein the reaction pressure is 0.5 to 1.1 MPa; the linear velocity of fluid at the nozzle of the Venturi ejector is controlled to be 105-120 m/s.

10. The method according to claim 9, wherein the mass ratio of p-nitrochlorobenzene to sodium hydroxide to ethanol is 1: 1.7: 2.5; in the etherification reaction process, the reaction pressure is controlled to be 0.8MPa, the reaction temperature is controlled to be 60 ℃, the reaction time is 50min, and the linear velocity of fluid at the nozzle of the Venturi ejector is controlled to be 113 m/s.