Continuous production device for o-hydroquinone and hydroquinone

Abstract

The utility model provides a continuous production device for o-hydroquinone and hydroquinone, and relates to the technical field of chemical synthesis. According to the utility model, phenol and hydrogen peroxide are used as raw materials, and high-purity catechol and hydroquinone products are continuously produced through the reactor, the filtering device, the hydrogen peroxide decomposition reactor, the extraction tower and the refining unit; by arranging the filter device, the extraction tower, the extraction agent recovery tower, the phenol removal tower I, the tar removal tower, the phenol removal tower II, the catechol tower, the light component removal tower and the hydroquinone tower, materials after reaction are separated and purified, high-purity catechol and hydroquinone products are obtained, the whole technological process is short, and the yield is high; according to the utility model, the extraction tower is adopted to replace the dehydration rectification operation in the traditional process to remove phenol-containing wastewater, so that the phenol recovery rate is improved, and the subsequent wastewater treatment burden is reduced; the detarring tower is placed in front of the second dephenolization tower, so that the retention time of tar impurities in the whole process system is shortened, and the safety of the whole process is improved.

Description

Technical Field

[0001] This utility model relates to the field of chemical synthesis technology, specifically to a continuous production apparatus for ortho- and hydroquinone. Background Technology

[0002] Hydroquinone is an important chemical raw material, widely used as a developer, preservative, rubber antioxidant, polymerization inhibitor, stabilizer in coatings and fragrances, and also in pesticides, flavorings, pharmaceuticals, and water treatment. Hydroquinone (1,4-dihydroxybenzene) and catechol (1,2-dihydroxybenzene) have similar structures and properties, and their derivatives are also widely used in various fields.

[0003] Currently, methods for synthesizing ortho- and hydroquinones include natural high-temperature treatment, hydrogen peroxide hydroxylation, and aniline oxidation, many of which have been industrialized. In the 1970s, a hydrogen peroxide hydroxylation technology was developed using phenol as a raw material and hydrogen peroxide as an oxidant. This method not only has low product cost and less solid waste, but also uses cheaper and more readily available raw materials, making it suitable for mass production.

[0004] However, existing hydrogen peroxide hydroxylation processes often use high-concentration hydrogen peroxide as raw material, posing an explosion hazard. Furthermore, to avoid generating large amounts of heavy components (tar) during the reaction, the conversion rate of phenol is controlled very low, resulting in high operating costs. Additionally, subsequent product separation and purification processes suffer from high energy consumption and difficulty in tar removal. For example, patent CN200610072928.6 discloses a separation and purification device and method for phenol, catechol / hydroquinone, and an aqueous tar solution. This method sequentially feeds the raw material liquid into a dehydration distillation column, a first dephenolization distillation column, a second dephenolization distillation column, a decoking distillation column, a deep distillation kettle, and a product rectification column. After rectification separation, catechol and hydroquinone are discharged from the top and bottom of the product distillation column, respectively. This method places the decoking distillation column after the second dephenolization column, increasing the difficulty of tar transportation and the operational risks of subsequent equipment. Utility Model Content

[0005] To address the shortcomings of existing technologies, this utility model discloses a continuous production apparatus for catechol and hydroquinone. The apparatus can effectively recover raw material phenol, thereby reducing the burden of subsequent wastewater treatment, reduce the residence time of tar in the process to improve operational safety, and continuously output high-purity hydroquinone and catechol products.

[0006] To achieve the above technical objectives, this utility model proposes a continuous production apparatus for o- and hydroquinone. The apparatus includes a reactor, a filtration device, a hydrogen peroxide decomposition reactor, an extraction tower, and a refining unit. The reactor is connected to a phenol input pipe, a hydrogen peroxide input pipe, and a catalyst slurry input pipe, and its outlet is connected to the inlet of the filtration device. The first outlet of the filtration device is used to output the filtered solid catalyst, and its second outlet is connected to the first inlet of the hydrogen peroxide decomposition reactor to output the filtered clarified liquid. The second inlet of the hydrogen peroxide decomposition reactor is connected to a sodium sulfite input pipe, and its outlet is connected to the first inlet of the extraction tower. The refining unit includes an extractant recovery tower, a phenol removal tower, a tar removal tower, a phenol removal tower, an o- and hydroquinone tower, a light oxidizing tower, and a hydroquinone tower. The second inlet of the extraction tower is connected to the extractant input pipe, and its upper outlet is connected to the inlet of the extractant recovery tower. The upper outlet of the extractant recovery tower is connected to a first phase separation device. The aqueous phase outlet of a phase-separating device is connected to the upper part of the extractant recovery tower, and its oil phase outlet outputs the recovered extractant; the bottom outlet of the extractant recovery tower is connected to the inlet of the phenol removal tower; the upper outlet of the phenol removal tower is connected to a second phase-separating device, the aqueous phase outlet of which outputs recovered water, and its oil phase outlet is connected to the upper part of the phenol removal tower, with a branch for outputting recovered phenol; the bottom outlet of the phenol removal tower is connected to the inlet of the tar removal tower. The upper outlet of the tar removal tower is connected to the inlet of the phenol removal tower. The bottom of the tar removal tower outputs impurities containing tar. The upper outlet of the phenol removal tower outputs recovered phenol, and its bottom outlet is connected to the inlet of the catechol tower. The upper outlet of the catechol tower outputs catechol product, and its bottom is connected to the inlet of the light component removal tower. The upper outlet of the light component removal tower outputs light component impurities, and its bottom is connected to the inlet of the hydroquinone tower. The upper outlet of the hydroquinone tower outputs hydroquinone product.

[0007] The continuous production process of ortho- and hydroquinone using the above technical solution includes the following steps:

[0008] The raw material phenol is preheated and then fed into the reactor along with hydrogen peroxide. Under the action of a catalyst, a hydroxylation reaction occurs, yielding a reacted material containing catechol, hydroquinone, hydrogen peroxide, water, catalyst, tar, quinone, and phenol. The reacted material is then fed into the filtration device.

[0009] After the reaction, the solid catalyst is separated by a filtration device, and the output catalyst can be directly returned to the reactor for recycling; the output filtrate enters the hydrogen peroxide decomposition reactor to decompose unreacted hydrogen peroxide.

[0010] In the hydrogen peroxide decomposition reactor, an excess of sodium sulfite solution relative to hydrogen peroxide is added to the filtrate through a sodium sulfite inlet pipe. The hydrogen peroxide in the filtrate is eliminated by an oxidation reaction to obtain the material to be extracted, thereby improving the safety of subsequent processes. The material to be extracted includes components such as catechol, hydroquinone, sodium sulfate, water, catalyst, tar, and phenol. This portion of the material to be extracted enters the extraction tower.

[0011] Inside the extraction tower, the material to be extracted is extracted with an extractant, and an oil phase containing o- and hydroquinones, phenol, water, tar, and extractant is extracted from the top of the tower. This oil phase is fed into the refining unit. An aqueous phase containing a small amount of sodium sulfate, a small amount of extractant, and water is collected from the bottom of the extraction tower. This invention uses an extraction tower instead of a dehydration distillation tower in the traditional process to remove phenol-containing wastewater from the reaction material. This not only reduces the overall energy consumption of the process but also significantly reduces the phenol content in the discharged wastewater, thereby reducing the burden on subsequent wastewater treatment.

[0012] In the refining unit, the oil phase containing the extractant output from the extraction tower is fed into the extractant recovery tower; the top product of the extractant recovery tower is subjected to phase separation treatment by the first phase separation device to obtain the extractant, and this portion of the extractant can be returned to the extraction process for recycling. The aqueous phase containing a small amount of extractant obtained from the phase separation is returned to the top of the extraction recovery tower as reflux; the bottom product of the extractant recovery tower is fed into the phenol removal tower.

[0013] The top of the phenol removal tower produces a mixture of phenol and water. This mixture is cooled and then enters the second phase separation unit. A portion of the phenol and other oil phases obtained from the phase separation are returned to the tower as reflux, while another portion is returned to the phenol feed tank or directly returned to the reactor for recycling. The aqueous phase obtained from the phase separation is recycled into the reaction process water tank. The material from the bottom of the phenol removal tower enters the tar removal tower.

[0014] The material containing tar and other contaminants collected from the bottom of the tar removal tower enters the tar post-processing stage, while the material collected from the top of the tar removal tower enters the phenol removal tower. This invention sets up a tar removal tower before the phenol removal tower, thereby effectively reducing the residence time of tar impurities in the process system and lowering the risks of subsequent operations.

[0015] Phenol is collected from the top of the second phenol removal tower and returned to the phenol raw material tank; the material collected from the bottom of the second phenol removal tower enters the catechol tower. This invention fully recovers unreacted phenol through the first and second phenol removal towers, achieving the recycling of raw materials, improving raw material utilization, and increasing the economic benefits of the process.

[0016] The top of the catechol column yields a catechol product with a mass fraction greater than 99.8%, while the bottom product is fed into a light component removal column for further removal of any light component impurities.

[0017] Light component impurities are collected from the top of the light component removal tower, and the bottom material is fed into the hydroquinone tower.

[0018] Hydroquinone with a mass fraction greater than 99.8% is collected from the top of the hydroquinone column, while heavy component impurities are collected from the bottom of the column.

[0019] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0020] This invention uses phenol and hydrogen peroxide as raw materials to continuously produce high-purity catechol and hydroquinone products through a reactor, filtration device, hydrogen peroxide decomposition reactor, extraction tower, and purification unit. By setting up a filtration device, extraction tower, extractant recovery tower, phenol removal tower, tar removal tower, phenol removal tower, catechol tower, light phenol removal tower, and hydroquinone tower to separate and purify the reactants, high-purity catechol and hydroquinone products are obtained. The overall process is short and has a high yield. This invention uses an extraction tower to replace the dehydration distillation operation in the traditional process to remove phenol-containing wastewater, improving phenol recovery rate and reducing the burden of subsequent wastewater treatment. Placing the tar removal tower before the phenol removal tower reduces the residence time of tar impurities in the overall process system, improving process safety and reducing the safety risks of subsequent operations. Attached Figure Description

[0021] The accompanying drawings, which form part of this application, are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an undue limitation of the present invention. In the drawings:

[0022] Figure 1 This diagram shows a structural diagram of a continuous production apparatus for ortho- and hydroquinone according to the present invention.

[0023] The above figures include the following reference numerals:

[0024] 1-Reactor, 2-Filtering device, 3-Hydrogen peroxide decomposition reactor, 4-Extraction tower, 51-Extractant recovery tower, 52-Phenol removal tower 1, 53-Tar removal tower, 54-Phenol removal tower 2, 55-Catechol tower, 56-Light component removal tower, 57-Cycloquinone tower, 6-Stripping tower, 71-First phase separation device, 72-Second phase separation device, S1-Phenol input pipe, S2-Hydrogen peroxide input pipe, S3-Catalyst slurry input pipe, S4-Catalyst recycling pipe, S5-Sodium sulfite input pipe, S6-Extractant input pipe, S7-Extractant recycling pipe, S8-Aqueous phase circulation pipe, S9-First phenol conveying pipe, S10-Tar conveying pipe, S11-Second phenol conveying pipe, S12-Catechol conveying pipe, S13-Light component impurity conveying pipe, S14-Cycloquinone conveying pipe, S15-Wastewater output pipe. Detailed Implementation

[0025] To facilitate understanding of this utility model, a more comprehensive description of it will be provided below, along with preferred embodiments. However, it should be understood that these embodiments are merely for more detailed explanation and should not be construed as limiting the utility model in any way, i.e., not limiting the scope of protection of this utility model.

[0026] Unless otherwise defined, the technical terms used in the following embodiments have the same meanings as commonly understood by those skilled in the art to which this invention pertains. Unless otherwise specified, the test reagents used in the following embodiments are conventional biochemical reagents; and the experimental methods, unless otherwise specified, are conventional methods.

[0027] Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first," "second," or "third" may explicitly or implicitly include one or more of that feature. In the description of this application, "a plurality of" means two or more, unless otherwise explicitly specified.

[0028] Example 1

[0029] A continuous production apparatus for ortho- and hydroquinones, such as Figure 1 As shown, the device includes a reactor 1, a filtration device 2, a hydrogen peroxide decomposition reactor 3, an extraction tower 4, and a purification unit, wherein:

[0030] Reactor 1 is connected to phenol input pipe S1, hydrogen peroxide input pipe S2 and catalyst slurry input pipe S3, and its outlet is connected to the inlet of filter device 2.

[0031] The first outlet of the filtration device 2 is used to output the solid catalyst obtained by filtration, and the second outlet is used to output the filtered clear liquid obtained by filtration. It is connected to the first inlet of the hydrogen peroxide decomposition reactor 3.

[0032] The second inlet of the hydrogen peroxide decomposition reactor 3 is connected to the sodium sulfite input pipe S5, and its outlet is connected to the first inlet of the extraction tower 4.

[0033] The refining unit includes an extractant recovery tower 51, a phenol removal tower 52, a tar removal tower 53, a phenol removal tower 54, a catechol removal tower 55, a light phenol removal tower 56, and a hydroquinone removal tower 57.

[0034] The second inlet of the extraction tower 4 is connected to the extractant input pipe S6, and its upper outlet is connected to the inlet of the extractant recovery tower 51.

[0035] The upper outlet of the extractant recovery tower 51 is connected to the first phase separation device 71. The aqueous phase outlet of the first phase separation device 71 is connected to the upper part of the extractant recovery tower 51, and the oil phase outlet outputs the recovered extractant. In an optional example of this utility model, the recovered extractant is fed into the extractant storage tank or directly returned to the extraction tower 4 through the extractant recycling pipe S7.

[0036] The bottom outlet of the extractant recovery tower 51 is connected to the inlet of the phenol removal tower 52.

[0037] The upper outlet of the phenol removal tower 52 is connected to the second phase separation device 72. The aqueous phase outlet of the second phase separation device 72 outputs recovered water, and its oil phase outlet is connected to the upper part of the phenol removal tower 52, and a branch is provided for outputting recovered phenol. The bottom outlet of the phenol removal tower 52 is connected to the inlet of the tar removal tower 53. In an optional example of this utility model, the phenol recovered by the phenol removal tower 52 is fed into the phenol storage tank through the first phenol conveying pipe S9 or directly returned to the reactor 1. The recovered water is fed into the circulating water storage tank through the aqueous phase circulation pipe S8 or directly returned to the catalyst slurry preparation process for preparing the catalyst slurry.

[0038] The upper outlet of the tar removal tower 53 is connected to the inlet of the phenol removal tower 54, and the bottom of the tar removal tower 53 outputs impurities containing tar. In an optional example of this utility model, these tar impurities are input into the subsequent tar treatment process through the tar conveying pipe S10.

[0039] The recovered phenol is output from the top of the phenol removal tower 54, and its bottom outlet is connected to the inlet of the catechol tower 55. In an optional example of this utility model, the phenol recovered from the phenol removal tower 54 is fed into the phenol storage tank via the second phenol conveying pipe S11 or directly returned to the reactor 1.

[0040] The upper part of the catechol tower 55 outputs catechol product, and its bottom is connected to the feed port of the light removal tower 56; in an optional example of this utility model, the catechol product is fed into the subsequent process through the catechol conveying pipe S12.

[0041] The upper part of the light component impurity output from the light component removal tower 56 is connected to the feed port of the hydroquinone tower 57; in an optional example of this utility model, this part of the light component impurity is input into the subsequent processing step via the light component impurity conveying pipe S13.

[0042] Hydroquinone product is output from the top of hydroquinone tower 57; in an optional example of this invention, the hydroquinone product is fed into subsequent processes via hydroquinone delivery pipe S14.

[0043] It should be noted that in this utility model, the "upper part" of the tower refers to the area from the middle of the tower's height to the top.

[0044] Furthermore, this invention does not limit the specific structure of reactor 1 and hydrogen peroxide decomposition reactor. Those skilled in the art can select reactor 1 suitable for the hydroxylation reaction of phenol and hydrogen peroxide and reactor suitable for hydrogen peroxide decomposition through non-creative labor, without limiting the scope of protection of this invention.

[0045] This utility model does not limit the specific structure of the filter device 2. Those skilled in the art can select a device or equipment that can achieve solid-liquid separation through non-creative labor, and this does not limit the scope of protection of this utility model.

[0046] Example 2

[0047] Based on the continuous production apparatus for ortho- and hydroquinone shown in Example 1, in this example, the bottom outlet of the hydroquinone tower 57 is connected to the detarting tower 53, thereby fully recovering the ortho- and hydroquinone, phenol and other components contained in the bottom product of the hydroquinone tower 57, improving the economic efficiency of the process; at the same time, the heavy components in the product of the hydroquinone tower 57 can be concentrated and combined with the heavy components such as tar in the detarting tower for processing, and the tar treatment efficiency can be improved by inputting it into the subsequent tar treatment program.

[0048] Example 3

[0049] Based on the continuous production apparatus for ortho- and hydroquinone shown in Example 1, the phenol removal tower 54 in this example is equipped with a side port for outputting light component impurities. By removing some light component impurities through the side port, the distillation separation effect of the phenol removal tower 54 can be improved, which is beneficial for further separation and recovery of phenol from the top of the tower. It is also beneficial for reducing the impurity content of species in the bottom of the tower, thereby improving the technical effect of separation and purification.

[0050] Furthermore, the side outlet of the phenol removal tower 54 is connected to the pipeline connecting the upper outlet of the light component removal tower 56, thereby combining the light component impurities output from the phenol removal tower 54 with those output from the light component removal tower 56 for processing, which improves the processing efficiency of subsequent light component impurity treatment processes.

[0051] Example 4

[0052] Based on the continuous production apparatus for o- and hydroquinone shown in Example 1, in this embodiment, the bottom outlet of the extraction tower 4 is connected to the stripping tower 6, and the bottom outlet of the stripping tower 6 outputs wastewater. This allows the stripping tower 6 to separate the oil phase material (extractant and target product) from the aqueous phase in the bottom of the extraction tower 4, further reducing the difficulty of subsequent wastewater treatment. The oil phase material output from the upper part of the stripping tower 6 can be recycled, improving the yield. In an optional example of this invention, this portion of wastewater is input into the subsequent wastewater treatment process through the wastewater output pipe S15.

[0053] Furthermore, the upper outlet of the stripping tower 6 is connected to the second phase separation device 72, and the aqueous phase outlet of the second phase separation device 72 is connected to the upper part of the stripping tower 6. This allows for the further recovery of the extractant contained in the bottom product of the extraction tower 4. After phase separation by the first phase separation device 71, the extractant can be recovered and reused.

[0054] Example 5

[0055] Based on the continuous production apparatus for ortho- and hydroquinone shown in Example 1, the solid catalyst obtained by filtration can be recycled by inputting it into the catalyst slurry preparation process through the catalyst recycling pipeline S4.

[0056] The continuous production apparatus for ortho- and hydroquinones in this embodiment also includes a catalyst activation unit, which is used to dry and calcine the solid catalyst output from the filter device 2 to activate it. When the activity of the catalyst obtained from the filter device 2 does not meet the standard for direct reuse, the catalyst can be dried and calcined by the catalyst activation unit to activate the catalyst for recycling.

[0057] In an optional example of this embodiment, the operation of the catalyst activation unit further includes washing the recovered catalyst with water to further remove impurities entrained on the catalyst surface and improve activation efficiency.

[0058] It should be noted that the present invention does not limit the specific structure of the catalyst activation unit. Those skilled in the art can select a device or equipment that can realize the drying, calcination and activation of solid catalysts as needed, without limiting the scope of protection of the present invention.

[0059] Example 6

[0060] Based on the continuous production apparatus for ortho- and hydroquinone shown in any one of Examples 1-5, this embodiment also includes a tail gas treatment unit for treating the tail gas output from reactor 1, filter device 2, hydrogen peroxide decomposition reactor 3 or stripping tower 6, and catalyst activation unit, thereby ensuring that the tail gas generated during the process meets emission requirements and improving the environmental friendliness of the process.

[0061] Furthermore, the exhaust gas treatment unit includes a water washing tower and an adsorption device. The outlet of the water washing tower is connected to the inlet of the adsorption device, and the treated exhaust gas is discharged from the outlet of the adsorption device.

[0062] It should be noted that this utility model does not limit the number of stages of the water washing tower. One or more water washing towers can be selected. When multiple stages of water washing towers are included, the first water washing tower is connected to the tail gas input pipe, and the outlet of the last water washing tower is connected to the inlet of the adsorption device. The treated tail gas is discharged from the outlet of the adsorption device.

[0063] Furthermore, this invention does not limit the materials and structure of the adsorption device; it can be selected from activated carbon adsorption devices, resin adsorption devices, etc., and those skilled in the art can choose according to their needs.

[0064] Example 7

[0065] Based on the continuous production apparatus for catechol and hydroquinone shown in Example 1, this example also includes a packaging unit for preparing and packaging the catechol and hydroquinone products output from catechol tower 55 and hydroquinone tower 57 into finished products.

[0066] It should be noted that this utility model does not limit the specific structure of the equipment included in the packaging unit. Those skilled in the art can select equipment and apparatus that can realize the packaging and sheeting of catechol and hydroquinone as needed, without limiting the scope of protection of this utility model.

[0067] It should be noted that the above description is a further detailed explanation of the present invention in conjunction with specific embodiments, and should not be construed as limiting the specific implementation of the present invention to these descriptions. For those skilled in the art, several simple improvements can be made without departing from the concept of the present invention, and all such improvements should be considered to fall within the scope of protection of the present invention.

Claims

1. A continuous production apparatus for o- and hydroquinone, characterized in that, It includes a reactor (1), a filtration device (2), a hydrogen peroxide decomposition reactor (3), an extraction tower (4), and a purification unit, wherein, The reactor (1) is connected to the phenol input pipe (S1), the hydrogen peroxide input pipe (S2) and the catalyst slurry input pipe (S3), and its outlet is connected to the inlet of the filter device (2). The first outlet of the filtration device (2) is used to output the solid catalyst obtained by filtration, and the second outlet of the filtration clear liquid obtained by filtration is connected to the first inlet of the hydrogen peroxide decomposition reactor (3). The second inlet of the hydrogen peroxide decomposition reactor (3) is connected to the sodium sulfite input pipe (S5), and its outlet is connected to the first inlet of the extraction tower (4); The refining unit includes an extractant recovery tower (51), a phenol removal tower (52), a tar removal tower (53), a phenol removal tower (54), a catechol tower (55), a light phenol removal tower (56), and a hydroquinone tower (57). The second inlet of the extraction tower (4) is connected to the extractant input pipe (S6), and its upper outlet is connected to the inlet of the extractant recovery tower (51). The upper outlet of the extractant recovery tower (51) is connected to the first phase separation device (71), the aqueous phase outlet of the first phase separation device (71) is connected to the upper part of the extractant recovery tower (51), and the oil phase outlet outputs the recovered extractant; the bottom outlet of the extractant recovery tower (51) is connected to the inlet of the phenol removal tower (52). The upper outlet of the phenol removal tower (52) is connected to the second phase separation device (72). The water phase outlet of the second phase separation device (72) outputs recovered water, and its oil phase outlet is connected to the upper part of the phenol removal tower (52), and a branch for outputting recovered phenol is provided. The bottom outlet of the phenol removal tower (52) is connected to the inlet of the tar removal tower (53). The upper outlet of the tar removal tower (53) is connected to the inlet of the phenol removal tower (54), and the bottom of the tar removal tower (53) outputs impurities containing tar. The recovered phenol is output from the top of the phenol removal tower (54), and its bottom outlet is connected to the feed inlet of the catechol tower (55). The upper part of the catechol tower (55) outputs catechol product, and its bottom is connected to the feed inlet of the light removal tower (56). The upper part of the light component impurity is output from the light component removal tower (56), and its bottom is connected to the feed port of the hydroquinone tower (57). The hydroquinone tower (57) outputs hydroquinone product from its upper part.

2. The continuous production apparatus for o- and hydroquinones according to claim 1, characterized in that, The bottom outlet of the hydroquinone tower (57) is connected to the tar removal tower (53).

3. The continuous production apparatus for o- and hydroquinones according to claim 1, characterized in that, The phenol removal tower (54) is equipped with a side sampling port for outputting light component impurities.

4. The continuous production apparatus for o- and hydroquinones according to claim 3, characterized in that, The side outlet of the phenol removal tower (54) is connected to the pipeline that connects to the upper outlet of the light removal tower (56).

5. The continuous production apparatus for o- and hydroquinones according to claim 1, characterized in that, The bottom outlet of the extraction tower (4) is connected to the stripping tower (6), and wastewater is discharged from the bottom outlet of the stripping tower (6).

6. The continuous production apparatus for o- and hydroquinones according to claim 5, characterized in that, The upper outlet of the stripping tower (6) is connected to the first phase separation device (71), and the water phase outlet of the first phase separation device (71) is connected to the upper part of the stripping tower (6).

7. The continuous production apparatus for o- and hydroquinones according to claim 1, characterized in that, It also includes a catalyst activation unit for activating the solid catalyst output from the filter device (2) by drying and calcining.

8. The continuous production apparatus for o- and hydroquinones according to any one of claims 1-7, characterized in that, It also includes an exhaust gas treatment unit for treating the exhaust gas output from the reactor (1), the filter device (2), the hydrogen peroxide decomposition reactor (3) or the stripping tower (6), and the catalyst activation unit.

9. The continuous production apparatus for o- and hydroquinones according to claim 8, characterized in that, The exhaust gas treatment unit includes a water washing tower and an adsorption device. The outlet of the water washing tower is connected to the inlet of the adsorption device, and the treated exhaust gas is discharged from the outlet of the adsorption device.

10. The continuous production apparatus for o- and hydroquinones according to claim 1, characterized in that, It also includes a packaging unit for sheet packaging the catechol and hydroquinone products output from the catechol tower (55) and the hydroquinone tower (57) to output the finished product.

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