Hydrogen peroxide production plant

Abstract

The embodiment of the application relates to the chemical technology field, and discloses a hydrogen peroxide production device, which comprises a first heat exchanger, the first heat exchanger comprises a first heat exchange body and a heat exchange pipeline, the first heat exchange body is provided with a first heat exchange cavity, at least part of the heat exchange pipeline is arranged in the first heat exchange cavity, a hydrogenation unit and an oxidation unit are in communication with the heat exchange pipeline, an inlet end of the first heat exchange cavity is in communication with an external water storage equipment, and an outlet end of the first heat exchange cavity is in communication with an absorption heat pump unit. According to the application, low-grade heat energy can be recycled and reused, heat energy loss is effectively avoided, energy is saved, energy saving and emission reduction of the hydrogen peroxide production device are facilitated, and the hydrogen peroxide production device has excellent energy saving value.

Description

Technical Field

[0001] This application relates to the field of chemical technology, and in particular to a hydrogen peroxide production apparatus. Background Technology

[0002] The anthraquinone process for producing hydrogen peroxide involves hydrogenation, oxidation, extraction, purification, and post-treatment. The hydrogenation, oxidation, and post-treatment processes all generate low-grade heat, consuming significant amounts of electricity. While existing hydrogen peroxide production facilities incorporate heat exchange systems to recover waste heat from each process, and energy-saving modifications can recover heat from the condensate in these systems, current facilities cannot efficiently recover and utilize the low-grade heat generated in each process, resulting in its waste. Therefore, how to efficiently recover and utilize the low-grade heat generated in each process is a pressing issue that needs to be addressed. Utility Model Content

[0003] Embodiments of this application provide a hydrogen peroxide production apparatus that helps to recover and reuse low-grade heat energy, thereby contributing to energy conservation and emission reduction in the hydrogen peroxide production apparatus.

[0004] To address the aforementioned technical problems, embodiments of this application disclose the following technical solutions:

[0005] On the one hand, a hydrogen peroxide production apparatus is provided, comprising: a hydrogenation unit, an oxidation unit, a first heat exchanger, and an absorption heat pump unit;

[0006] The first heat exchanger includes: a first heat exchange body and heat exchange pipelines. The first heat exchange body is provided with a first heat exchange cavity. At least part of the heat exchange pipelines are provided in the first heat exchange cavity. The hydrogenation unit and the oxidation unit are both connected to the heat exchange pipelines. The inlet end of the first heat exchange cavity is connected to an external water storage device. The outlet end of the first heat exchange cavity is connected to an absorption heat pump unit.

[0007] In addition to one or more of the features disclosed above, or as an alternative, the heat exchange pipeline includes: a first heat exchange pipeline and a second heat exchange pipeline, at least a portion of the first heat exchange pipeline being disposed in the first heat exchange chamber, the inlet end of the first heat exchange pipeline being connected to the hydrogenation unit, the outlet end of the first heat exchange pipeline being connected to the oxidation unit, at least a portion of the second heat exchange pipeline being disposed in the first heat exchange chamber, and the inlet end of the second heat exchange pipeline being connected to the oxidation unit.

[0008] In addition to one or more of the features disclosed above, or as an alternative, the absorption heat pump unit includes: a generator, a condenser, an absorber, and an evaporator.

[0009] The generator is connected to the outlet end of the first heat exchange chamber, the condenser and the absorber respectively. The condenser is connected to the external condensate circulation equipment and the evaporator respectively. The absorber is connected to the evaporator. The generator contains a concentrated lithium bromide solution and the absorber contains a dilute lithium bromide solution.

[0010] In addition to one or more of the features disclosed above, or as an alternative, the generator includes: a generator body, provided with a first cavity, the first cavity being connected to an absorber, and the first cavity storing a concentrated lithium bromide solution;

[0011] A third heat exchange pipeline, at least partially disposed within the first cavity, is connected to both the outlet end of the first heat exchange cavity and an external water storage device; and

[0012] The first spray section is disposed in the first cavity and is connected to the absorber;

[0013] The condenser includes: a condenser body, a condensation chamber connected to a first chamber and an evaporator; and

[0014] The condenser piping, at least part of which is located inside the condenser chamber, is connected to an external condensate circulation system.

[0015] In addition to one or more of the features disclosed above, or as an alternative, the absorber includes: an absorber body, a second cavity provided therein, the second cavity being in communication with the first spray section, and the second cavity storing a dilute lithium bromide solution.

[0016] A fourth heat exchange pipe, at least a portion of which is located in the second cavity, is configured to circulate the fluid to be heated; and

[0017] The second spray section is disposed in the second cavity and is connected to the first cavity;

[0018] The evaporator includes: an evaporator body, an evaporation chamber, and a second chamber connected to the evaporation chamber;

[0019] The fifth heat exchange pipeline, at least a portion of which is located within the evaporation chamber; and

[0020] The third spray section is located in the evaporation chamber and is connected to the condensation chamber.

[0021] In addition to one or more of the features disclosed above, or as an alternative, the absorption heat pump unit further includes: a second heat exchanger, the second heat exchanger including: a second heat exchange shell and a sixth heat exchange pipe, the second heat exchange shell being provided with a second heat exchange cavity, the second heat exchange cavity being connected to a second cavity body and a first spray section respectively, at least a portion of the sixth heat exchange pipe being provided in the second heat exchange cavity, and the sixth heat exchange pipe being connected to the first cavity body and the second spray section respectively.

[0022] In addition to one or more of the features disclosed above, or as an alternative, it also includes: an extraction tower, the inlet of which is connected to the outlet of the second heat exchange pipeline and an external water storage device, respectively.

[0023] The purification tower has its inlet connected to the outlet of the extraction tower.

[0024] The hydrogen peroxide storage unit is connected to the outlet of the purification tower;

[0025] The alkali tower has its inlet connected to both the outlet of the extraction tower and the concentrated alkali storage tank.

[0026] An alkali settling device, the inlet of which is connected to the outlet of the alkali tower; and

[0027] The third heat exchanger is connected to the outlet of the alkali settler and the fifth heat exchange pipeline.

[0028] In addition to one or more of the features disclosed above, or alternatively, it also includes: a raffinate separator, which is connected to the outlet of the extraction tower and the inlet of the alkali tower, respectively.

[0029] Post-treatment white clay bed, which is connected to the outlet end of the alkali settling device;

[0030] The regenerated liquid collector is connected to the post-treatment clay bed.

[0031] In addition to one or more of the features disclosed above, or as an alternative, the third heat exchanger includes: a first heat exchange section and a second heat exchange section, the first heat exchange section being provided with a first heat exchange channel, the second heat exchange section being provided within the first heat exchange channel and having a second heat exchange channel, the first heat exchange channel being connected to the outlet end of the alkali settler and the external atmospheric space respectively, and the second heat exchange channel being connected to the external water storage equipment and the fifth heat exchange pipeline respectively.

[0032] In addition to one or more of the features disclosed above, or as an alternative, the hydrogenation unit includes: a hydrogenation tower, a regenerated liquid storage tank, a heater, a filter, and a hydrogenated clay bed. The inlet end of the hydrogenation tower is connected to an external hydrogen storage device. The regenerated liquid storage tank is connected to the inlet end of the hydrogenation tower via the heater. The filter is connected to the outlet end of the hydrogenation tower and the hydrogenated clay bed, respectively. The hydrogenated clay bed is connected to the inlet end of the first heat exchange pipeline.

[0033] The oxidation unit includes an oxidation tower, a separator, an exhaust gas processor, and an oxidation liquid storage tank. The inlet end of the oxidation tower is connected to the outlet end of the first heat exchange pipeline and the external atmospheric space, respectively. The outlet end of the oxidation tower is connected to the inlet end of the separator. The outlet end of the separator is connected to the exhaust gas processor and the oxidation liquid storage tank, respectively. The oxidation liquid storage tank is also connected to the inlet end of the second heat exchange pipeline.

[0034] One of the above technical solutions has the following advantages or beneficial effects: By setting up a first heat exchanger and an absorption heat pump unit, the first heat exchanger is used to initially recover low-grade heat energy from the hydrogenated liquid and the oxidized liquid. Then, the absorption heat pump unit is used to convert the low-grade heat energy into high-temperature heat energy, so that the heat energy can be recovered and used for other production processes. This helps to recover and reuse low-grade heat energy, effectively avoids heat energy loss, and thus saves energy. It also helps to save energy and reduce emissions in the hydrogen peroxide production unit, making the hydrogen peroxide production unit have excellent energy-saving value. Attached Figure Description

[0035] The technical solution and other beneficial effects of this application will become apparent from the following detailed description of specific embodiments in conjunction with the accompanying drawings.

[0036] Figure 1 This is a schematic diagram of the structure of a hydrogen peroxide production apparatus provided according to an embodiment of this application;

[0037] Figure 2 This is a schematic diagram of the structure of an absorption heat pump unit according to an embodiment of this application;

[0038] Figure 3 This is a thermal energy flow diagram of a hydrogen peroxide production apparatus provided according to an embodiment of this application.

[0039] Explanation of reference numerals in the attached figures:

[0040] 100. Hydrogen peroxide production unit; 110. Hydrogenation unit; 111. Hydrogenation tower; 112. Regenerated liquid storage tank; 113. Heater; 114. Filter; 115. Hydrogenated clay bed; 116. Hydrogen compressor; 117. Hydrogenated liquid pump; 120. Oxidation unit; 121. Oxidation tower; 122. Separator; 123. Tail gas processor; 124. Oxidation liquid storage tank; 125. Air compressor; 126. Oxidation liquid pump; 130. First heat exchanger; 131. First heat exchanger body; 1311. First heat exchange chamber; 132. Heat exchange piping; 1321, First heat exchange piping; 1322, Second heat exchange piping; 133, First water pump; 140, Absorption heat pump unit; 141, Generator; 1411, Generator body; 1412, First cavity; 1413, Third heat exchange piping; 1414, First spray section; 142, Condenser; 1421, Condenser body; 1422, Condensation chamber; 1423, Condensation piping; 143, Absorber; 1431, Absorber body; 1432, Second cavity; 1433, Fourth heat exchange piping; 1434, First... Second spray section; 144, Evaporator; 1441, Evaporator body; 1442, Evaporation chamber; 1443, Fifth heat exchange pipeline; 1444, Third spray section; 145, Second heat exchanger; 1451, Second heat exchange shell; 1452, Second heat exchange chamber; 1453, Sixth heat exchange pipeline; 1461, First drain pump; 1462, Refrigerant pump; 1463, Concentrated solution pump; 1464, Dilute solution pump; 1465, Second drain pump; 150, Extraction unit; 151, Extraction tower; 152, Raffinate separator; 153, Pure water pump ; 160. Purification unit; 161. Purification tower; 162. Hydrogen peroxide storage tank; 170. Post-treatment unit; 171. Alkali tower; 172. Alkali solution settling tank; 173. Post-treatment clay bed; 174. Regenerated liquid collector; 175. Concentrated alkali storage tank; 176. Alkali pump; 177. Alkali solution pump; 178. Air pump; 180. Third heat exchanger; 181. First heat exchange section; 1811. First heat exchange channel; 182. Second heat exchange section; 1821. Second heat exchange channel; 183. Second water pump; 184. Third water pump. Detailed Implementation

[0041] To make the objectives, technical solutions, and beneficial effects of this application clearer, the following detailed description, in conjunction with the accompanying drawings and specific embodiments, further illustrates this application. It should be understood that the specific embodiments described in this specification are merely for explaining this application and are not intended to limit it.

[0042] In the description of this application, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," and "counterclockwise," etc., indicating orientation or positional relationships based on the orientation or positional relationships shown in the accompanying drawings, are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this application. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, features defined with "first" and "second" may explicitly or implicitly include one or more of the stated features. In the description of this application, "a plurality of" means two or more, unless otherwise explicitly specified.

[0043] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection, a direct connection, or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0044] In this application, unless otherwise expressly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature being directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature being directly above or diagonally above the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0045] To address the issue of unrecoverable low-grade waste heat generated during hydrogen peroxide production, in the embodiments of this application, referring to... Figure 1 This application provides a hydrogen peroxide production apparatus 100, which includes: a hydrogenation unit 110, an oxidation unit 120, a first heat exchanger 130, and an absorption heat pump unit 140.

[0046] Specifically, the hydrogenation unit 110 is configured to hydrogenate hydrogen to generate hydrogenated liquid, the oxidation unit 120 is configured to oxidize the hydrogenated liquid to generate oxidized liquid, and the first heat exchanger 130 and the absorption heat pump unit 140 are both configured to recover heat energy from the hydrogenated liquid and the oxidized liquid. Specifically, the first heat exchanger 130 and the absorption heat pump unit 140 are both configured to recover low-grade heat energy from the hydrogenated liquid and the oxidized liquid.

[0047] Specifically, the first heat exchanger 130 includes: a first heat exchange body 131 and a heat exchange pipeline 132. The first heat exchange body 131 is provided with a first heat exchange chamber 1311. At least part of the heat exchange pipeline 132 is provided in the first heat exchange chamber 1311. The hydrogenation unit 110 and the oxidation unit 120 are both connected to the heat exchange pipeline 132. The inlet end of the first heat exchange chamber 1311 is connected to an external water storage device. The outlet end of the first heat exchange chamber 1311 is connected to the absorption heat pump unit 140.

[0048] The first heat exchanger 130 can be a conventional shell-and-tube heat exchanger, but is not limited to this.

[0049] The absorption heat pump unit 140 can be a type II lithium bromide absorption heat pump unit, but is not limited thereto.

[0050] Understandably, when the hydrogenation unit 110 hydrogenates hydrogen to produce hydrogenated liquid, it releases heat and generates low-grade heat energy. Similarly, when the oxidation unit 120 oxidizes hydrogenated liquid to produce oxidized liquid, it also releases heat and generates low-grade heat energy. However, existing production equipment cannot effectively recover and utilize low-grade heat energy.

[0051] In this application, the hydrogenation unit 110 hydrogenates hydrogen to generate hydrogenated liquid and produces low-grade heat energy. The oxidation unit 120 oxidizes the hydrogenated liquid to generate oxidized liquid and produces low-grade heat energy. The hydrogenated liquid and the oxidized liquid with low-grade heat energy are respectively transported to the heat exchange pipeline 132. An external water storage device transports water to the first heat exchange chamber 1311. The water in the first heat exchange chamber 1311 exchanges heat with the hydrogenated liquid and the oxidized liquid in the heat exchange pipeline 132 to absorb the low-grade heat energy of the hydrogenated liquid and the oxidized liquid. The water that has completed the heat exchange is transported to the absorption heat pump unit 140 to further convert the heat energy of the water that has completed the heat exchange into high-temperature heat energy for recovery and utilization.

[0052] This application, by setting up a first heat exchanger 130 and an absorption heat pump unit 140, utilizes the first heat exchanger 130 to initially recover low-grade heat energy from the hydrogenation liquid and oxidation liquid, and then uses the absorption heat pump unit 140 to convert the low-grade heat energy into high-temperature heat energy, so that the heat energy can be recovered and used for other production processes. This helps to recover and reuse low-grade heat energy, effectively avoids heat energy loss, and thus saves energy. It also contributes to the energy conservation and emission reduction of the hydrogen peroxide production device 100, making the hydrogen peroxide production device 100 have excellent energy-saving value.

[0053] In some embodiments, refer to Figure 1 The heat exchange pipeline 132 includes: a first heat exchange pipeline 1321 and a second heat exchange pipeline 1322. At least a portion of the first heat exchange pipeline 1321 is disposed in the first heat exchange chamber 1311. The inlet end of the first heat exchange pipeline 1321 is connected to the hydrogenation unit 110, and the outlet end of the first heat exchange pipeline 1321 is connected to the oxidation unit 120. At least a portion of the second heat exchange pipeline 1322 is disposed in the first heat exchange chamber 1311, and the inlet end of the second heat exchange pipeline 1322 is connected to the oxidation unit 120.

[0054] The first heat exchange pipe 1321 and the second heat exchange pipe 1322 may be made of a thermally conductive material. For example, the first heat exchange pipe 1321 and the second heat exchange pipe 1322 may be made of copper, but are not limited thereto.

[0055] Understandably, the hydrogenation unit 110 hydrogenates hydrogen to generate hydrogenated liquid and produces low-grade heat energy. The oxidation unit 120 oxidizes the hydrogenated liquid to generate oxidized liquid and produces low-grade heat energy. The hydrogenated liquid with low-grade heat energy is transported to the first heat exchange pipeline 1321, and the oxidized liquid with low-grade heat energy is transported to the second heat exchange pipeline 1322. An external water storage device transports water to the first heat exchange chamber 1311. The water in the first heat exchange chamber 1311 exchanges heat with the hydrogenated liquid in the first heat exchange pipeline 1321 and the oxidized liquid in the second heat exchange pipeline 1322 to absorb the low-grade heat energy of the hydrogenated liquid and the oxidized liquid. The water that has completed the heat exchange is transported to the absorption heat pump unit 140.

[0056] This application establishes a first heat exchange chamber 1311 through which water flows, a first heat exchange pipe 1321 through which a low-grade heat-energy hydrogenated liquid flows, and a second heat exchange pipe 1322 through which a low-grade heat-energy oxidizing liquid flows. This allows heat exchange between the water in the first heat exchange chamber 1311 and the hydrogenated liquid in the first heat exchange pipe 1321 and the oxidizing liquid in the second heat exchange pipe 1322. This enables the preliminary recovery and utilization of low-grade heat energy in the hydrogenated liquid and oxidizing liquid, effectively avoiding heat loss and saving energy. This contributes to the energy conservation and emission reduction of the hydrogen peroxide production device 100, giving the hydrogen peroxide production device 100 excellent energy-saving value.

[0057] In some embodiments, refer to Figure 1 The first heat exchanger 130 further includes a first water pump 133, which is disposed between the inlet end of the first heat exchange chamber 1311 and the external water storage device. The first water pump 133 is connected to the inlet end of the first heat exchange chamber 1311 and the external water storage device respectively. The first water pump 133 transports water from the external water storage device to the first heat exchange chamber 1311, which helps to improve the efficient flow of water in the first heat exchange chamber 1311 and improves the heat exchange effect of the first heat exchanger 130.

[0058] In some embodiments, refer to Figure 1 The hydrogenation unit 110 includes: a hydrogenation tower 111, a regenerated liquid storage tank 112, a heater 113, a filter 114, and a hydrogenated clay bed 115.

[0059] Specifically, the inlet end of the hydrogenation tower 111 is connected to an external hydrogen storage device, the regenerated liquid storage tank 112 is connected to the inlet end of the hydrogenation tower 111 through the heater 113, the filter 114 is connected to the outlet end of the hydrogenation tower 111 and the hydrogenated clay bed 115 respectively, and the hydrogenated clay bed 115 is connected to the inlet end of the first heat exchange pipeline 1321.

[0060] The regenerated liquid storage tank 112 contains regenerated liquid, which includes, but is not limited to, ethyl anthraquinone.

[0061] Understandably, pure hydrogen from the external hydrogen storage device is transported to the hydrogenation tower 111, and the regenerated liquid from the regenerated liquid storage tank 112 is transported to the heater 113. After being preheated to a certain temperature by the heater 113, it is transported to the hydrogenation tower 111. The hydrogen gas in the hydrogenation tower 111 reacts with ethyl anthraquinone in the regenerated liquid to obtain hydrogenated liquid. The generated hydrogenated liquid is transported to the filter 114. After being filtered by the filter 114, it flows evenly into the hydrogenated clay bed 115 and is then transported to the first heat exchange pipeline 1321 of the first heat exchanger 130 to exchange heat with the water in the first heat exchange chamber 1311. The hydrogenated liquid is cooled, and the water in the first heat exchange chamber 1311 is heated. After the heat exchange is completed, the hydrogenated liquid is transported to the oxidation tower 121, and the water in the first heat exchange chamber 1311 is transported to the absorption heat pump unit 140.

[0062] In some embodiments, refer to Figure 1The hydrogenation unit 110 also includes a hydrogen compressor 116 and a hydrogenation liquid pump 117. The hydrogen compressor 116 is connected to the inlet of the external hydrogen storage equipment and the hydrogenation tower 111, respectively, to compress the excess pure hydrogen in the external hydrogen storage equipment into hydrogen gas at a certain pressure and deliver it to the hydrogenation tower 111. The hydrogenation liquid pump 117 is connected to the inlet of the hydrogenation clay bed 115 and the first heat exchange pipeline 1321, respectively, to deliver the hydrogenated liquid treated by the hydrogenation clay bed 115 to the first heat exchange pipeline 1321 of the first heat exchanger 130.

[0063] In some embodiments, refer to Figure 1 The oxidation unit 120 includes: an oxidation tower 121, a separator 122, an exhaust gas processor 123, and an oxidation liquid storage tank 124.

[0064] Specifically, the inlet end of the oxidation tower 121 is connected to the outlet end of the first heat exchange pipeline 1321 and the external atmospheric space, the outlet end of the oxidation tower 121 is connected to the inlet end of the separator 122, the outlet end of the separator 122 is connected to the exhaust gas processor 123 and the oxidation liquid storage tank 124, and the oxidation liquid storage tank 124 is also connected to the inlet end of the second heat exchange pipeline 1322.

[0065] Among them, the exhaust gas treatment device 123 can be a carbon fiber exhaust gas treatment device, but is not limited to it.

[0066] Understandably, after heat exchange, the hydrogenated liquid is transported to the oxidation tower 121, and air is also transported to the oxidation tower 121. The air and hydrogenated liquid undergo an oxidation reaction at a set temperature and pressure to generate an oxidized liquid. The generated oxidized liquid is transported to the separator 122, where it undergoes gas-liquid separation. The exhaust gas obtained from the separator 122 is transported to the exhaust gas processor 123, where it is processed and then discharged into the air. The oxidized liquid after separating the exhaust gas is transported to the oxidized liquid storage tank 124, and then transported to the second heat exchange pipeline 1322 of the first heat exchanger 130 to exchange heat with the water in the first heat exchange chamber 1311. The oxidized liquid is cooled, and the water in the first heat exchange chamber 1311 is heated. After heat exchange, the oxidized liquid is transported to the subsequent processing device, and the water in the first heat exchange chamber 1311 is transported to the absorption heat pump unit 140.

[0067] In some embodiments, refer to Figure 1The oxidation unit 120 also includes an air compressor 125 and an oxidation liquid pump 126. The air compressor 125 is connected to the inlet end of the oxidation tower 121 and the external atmospheric space, respectively. The air compressor 125 is used to compress air and deliver it into the oxidation tower 121. The oxidation liquid pump 126 is connected to the inlet end of the oxidation liquid storage tank 124 and the second heat exchange pipeline 1322, respectively. The oxidation liquid pump 126 is used to deliver the oxidation liquid in the oxidation liquid storage tank 124 to the second heat exchange pipeline 1322 of the first heat exchanger 130, which helps the oxidation liquid flow efficiently.

[0068] In some embodiments, refer to Figure 1 The absorption heat pump unit 140 includes: a generator 141, a condenser 142, an absorber 143, and an evaporator 144.

[0069] Specifically, the generator 141 is connected to the outlet end of the first heat exchange chamber 1311, the condenser 142 and the absorber 143 respectively. The condenser 142 is connected to the external condensate circulation equipment and the evaporator 144 respectively. The absorber 143 is connected to the evaporator 144. The generator 141 stores a concentrated lithium bromide solution and the absorber 143 stores a dilute lithium bromide solution.

[0070] Understandably, the water that has undergone heat exchange in the first heat exchange chamber 1311 is transported to the generator 141, and the dilute lithium bromide solution located in the absorber 143 is also transported to the generator 141. The dilute lithium bromide solution exchanges heat with the water that has undergone heat exchange. After heating, the dilute lithium bromide solution is concentrated into a concentrated lithium bromide solution, while simultaneously generating steam. The steam is transported to the condenser 142, and an external condensate circulation device transports condensate to the condenser 142. The steam and condensate undergo heat exchange, and the steam is condensed into refrigerant water. The refrigerant water is then transported to the evaporator 144 for further processing. The vapor in evaporator 144 is re-evaporated into steam and then transported to absorber 143. The heated concentrated lithium bromide solution is then transported to absorber 143, where it absorbs the steam to dilute it into a dilute lithium bromide solution. Simultaneously, heat is released to heat other production processes within absorber 143, thereby achieving the recovery and utilization of low-grade heat energy. This effectively avoids heat loss, saves energy, and contributes to the energy conservation and emission reduction of hydrogen peroxide production unit 100, giving it excellent energy-saving value.

[0071] In some embodiments, refer to Figure 2The generator 141 includes: a generator body 1411, a third heat exchange pipeline 1413, and a first spray section 1414. The generator body 1411 is provided with a first cavity 1412, which is connected to the absorber 143, and the first cavity 1412 stores a concentrated lithium bromide solution. At least a portion of the third heat exchange pipeline 1413 is disposed in the first cavity 1412, and the third heat exchange pipeline 1413 is connected to the outlet end of the first heat exchange cavity 1411 and an external water storage device, respectively. The first spray section 1414 is disposed in the first cavity 1412 and is connected to the absorber 143.

[0072] Specifically, the condenser 142 includes: a condenser body 1421 and a condenser pipe 1423. The condenser body 1421 is provided with a condensation chamber 1422, which is connected to the first chamber 1412 and the evaporator 144 respectively. The condenser pipe 1423 is at least partially disposed in the condensation chamber 1422 and is connected to an external condensate circulation device.

[0073] Understandably, the water that has completed heat exchange in the first heat exchange chamber 1311 is transported to the third heat exchange pipe 1413, and the dilute lithium bromide solution located in the absorber 143 is transported to the first spray section 1414. The first spray section 1414 sprays the dilute lithium bromide solution into the first chamber 1412, so that the dilute lithium bromide solution comes into contact with the third heat exchange pipe 1413. The dilute lithium bromide solution exchanges heat with the water that has completed heat exchange in the third heat exchange pipe 1413. After heating, the dilute lithium bromide solution is concentrated into a concentrated lithium bromide solution, and steam is generated at the same time. The steam is transported to the condenser 142, and the external condensate circulation equipment transports the condensate to the condenser pipe 1423. The steam comes into contact with the condenser pipe 1423, so that the steam and the condensate exchange heat. The steam is condensed into refrigerant water, which is transported to the evaporator 144, and the heated concentrated lithium bromide solution is transported to the absorber 143.

[0074] In some embodiments, refer to Figure 2 The absorber 143 includes: an absorber body 1431, a fourth heat exchange pipe 1433, and a second spray section 1434. The absorber body 1431 is provided with a second cavity 1432, which is connected to the first spray section 1414, and the second cavity 1432 stores a dilute lithium bromide solution. At least a portion of the fourth heat exchange pipe 1433 is provided in the second cavity 1432, and the fourth heat exchange pipe 1433 is configured to allow the flow of the fluid to be heated. The second spray section 1434 is provided in the second cavity 1432 and is connected to the first cavity 1412.

[0075] The fluid that can flow through the fourth heat exchange pipe 1433 can be a regenerated liquid.

[0076] Specifically, the evaporator 144 includes: an evaporator body 1441, a fifth heat exchange pipe 1443, and a third spray section 1444. The evaporator body 1441 is provided with an evaporation chamber 1442, which is connected to the second chamber 1432. At least a portion of the fifth heat exchange pipe 1443 is disposed in the evaporation chamber 1442, and the fifth heat exchange pipe 1443 is configured to circulate a fluid with low-grade heat energy. The third spray section 1444 is disposed in the evaporation chamber 1442 and is connected to the condensation chamber 1422.

[0077] Understandably, refrigerant water is transported to the third spray section 1444 of the evaporator 144, which sprays the refrigerant water into the evaporation chamber 1442 to contact the fifth heat exchange pipe 1443, allowing heat exchange between the refrigerant water and the fluid with low-grade heat energy in the fifth heat exchange pipe 1443. The refrigerant water is heated and evaporated into steam. The steam in the evaporator 144 is transported to the second chamber 1432 of the absorber 143, and the heated lithium bromide concentrated solution is transported to the second spray section 1434 of the absorber 143. The spray section 1434 sprays a concentrated lithium bromide solution into the second chamber 1432, allowing the concentrated lithium bromide solution to come into contact with steam. The concentrated lithium bromide solution absorbs the steam to dilute it into a dilute lithium bromide solution, while simultaneously releasing heat to heat the fluids to be heated in other production processes flowing through the fourth heat exchange pipeline 1433. This ultimately achieves the recovery and utilization of low-grade heat energy, effectively avoiding heat loss and saving energy. This contributes to the energy conservation and emission reduction of the hydrogen peroxide production unit 100, giving the hydrogen peroxide production unit 100 excellent energy-saving value.

[0078] In some embodiments, refer to Figure 2 The absorption heat pump unit 140 further includes a second heat exchanger 145, which includes a second heat exchange shell 1451 and a sixth heat exchange pipe 1453. The second heat exchange shell 1451 is provided with a second heat exchange cavity 1452, which is connected to the second cavity 1432 and the first spray section 1414 respectively. At least a portion of the sixth heat exchange pipe 1453 is provided in the second heat exchange cavity 1452, and the sixth heat exchange pipe 1453 is connected to the first cavity 1412 and the second spray section 1434 respectively.

[0079] Understandably, the dilute lithium bromide solution in the second chamber 1432 of the absorber 143 is first transported to the second heat exchange chamber 1452, and the concentrated lithium bromide solution in the first chamber 1412 of the generator 141 is transported to the sixth heat exchange pipe 1453. The dilute lithium bromide solution in the second heat exchange chamber 1452 and the concentrated lithium bromide solution in the sixth heat exchange pipe 1453 exchange heat. The dilute lithium bromide solution after heat exchange is transported to the first spray section 1414 to spray into the first chamber 1412, and the concentrated lithium bromide solution after heat exchange is transported to the second spray section 1434 to spray into the second chamber 1432, thereby helping the absorption heat pump unit 140 to recover and utilize low-grade heat energy.

[0080] In some embodiments, refer to Figures 1 to 2 The absorption heat pump unit 140 further includes: a first drain pump 1461, a refrigerant pump 1462, a concentrated solution pump 1463, a dilute solution pump 1464, and a second drain pump 1465. The first drain pump 1461 is connected to the outlet end of the third heat exchange pipeline 1413 to transport the water that has undergone heat exchange in the third heat exchange pipeline 1413 to external equipment; the refrigerant pump 1462 is connected to the condensing chamber 1422 and the third spray section 1444 respectively to transport the refrigerant water in the condensing chamber 1422 to the third spray section 1444; the concentrated solution pump 1463 is connected to the generator... The first chamber 1412 of the generator 141 is connected to the sixth heat exchange pipeline 1453 to transport the concentrated lithium bromide solution in the first chamber 1412 to the sixth heat exchange pipeline 1453; the dilute solution pump 1464 is connected to the second chamber 1432 and the second heat exchange chamber 1452 of the absorber 143 to transport the dilute lithium bromide solution in the second chamber 1432 to the second heat exchange chamber 1452; the second drain pump 1465 is connected to the outlet end of the fifth heat exchange pipeline 1443 to transport the fluid in the fifth heat exchange pipeline 1443 to external equipment.

[0081] In some embodiments, refer to Figure 1 The hydrogen peroxide production unit 100 also includes an extraction unit 150, a purification unit 160, a post-treatment unit 170, and a third heat exchanger 180.

[0082] Specifically, the extraction unit 150 includes an extraction tower 151 and a raffinate separator 152. The inlet end of the extraction tower 151 is connected to the outlet end of the second heat exchange pipeline 1322 and an external water storage device, respectively. The raffinate separator 152 is connected to the outlet end of the extraction tower 151.

[0083] Understandably, water from an external water storage device is transported to the extraction tower 151, and the oxidized liquid after heat exchange is also transported to the extraction tower 151. The oxidized liquid and water are in countercurrent contact in the extraction tower 151 to complete the extraction, obtaining a hydrogen peroxide solution of appropriate concentration and raffinate. The raffinate is transported to the raffinate separator 152, and the raffinate after being processed by the raffinate separator 152 is transported to the post-processing unit 170.

[0084] Specifically, the purification unit 160 includes a purification tower 161 and a hydrogen peroxide storage tank 162. The inlet end of the purification tower 161 is connected to the outlet end of the extraction tower 151, and the hydrogen peroxide storage tank 162 is connected to the outlet end of the purification tower 161.

[0085] Understandably, the hydrogen peroxide solution of appropriate concentration in the extraction tower 151 is transported to the purification tower 161. The purification tower 161 is equipped with a solvent oil column. The hydrogen peroxide solution settles to the bottom of the purification tower 161 by utilizing the difference in specific gravity, so that the impurities are dissolved by the solvent. After purification, the hydrogen peroxide solution is transported to the hydrogen peroxide storage tank 162 for storage.

[0086] Specifically, the post-processing unit 170 includes: an alkali tower 171, an alkali settling tank 172, a post-processing clay bed 173, a regenerated liquid collector 174, and a concentrated alkali storage tank 175. The inlet end of the alkali tower 171 is connected to the outlet end of the extraction tower 151. Specifically, the inlet end of the alkali tower 171 is connected to the raffinate separator 152, that is, the inlet end of the alkali tower 171 is connected to the outlet end of the extraction tower 151 through the raffinate separator 152. The inlet end of the alkali tower 171 is also connected to the concentrated alkali storage tank 175. The inlet end of the alkali settling tank 172 is connected to the outlet end of the alkali tower 171. The post-processing clay bed 173 is connected to the outlet end of the alkali settling tank 172. The regenerated liquid collector 174 is connected to the post-processing clay bed 173.

[0087] Understandably, the concentrated alkali solution in the concentrated alkali storage tank 175 is transported to the alkali tower 171. The raffinate after being treated by the raffinate separator 152 is also transported to the alkali tower 171. The concentrated alkali solution and the raffinate react in the alkali tower 171 to remove hydrogen peroxide from the raffinate. The raffinate after being treated in the alkali tower 171 is transported to the alkali settling tank 172 for thermal decomposition. The waste gas generated by thermal decomposition is transported to the third heat exchanger 180. The raffinate after dehydration and degassing in the alkali settling tank 172 is transported to the post-treatment bleaching clay bed 173. The raffinate is dehydrogenated in the post-treatment bleaching clay bed 173 to generate ethyl anthraquinone. The ethyl anthraquinone obtained in the post-treatment bleaching clay bed 173 is transported to the regenerated liquid collector 174 to prepare regenerated liquid, which can then flow back into the regenerated liquid storage tank 112 for later use.

[0088] In some embodiments, the extraction unit 150 further includes a pure water pump 153, which is connected to the inlet end of the extraction tower 151 and an external water storage device, respectively, to transport water from the external water storage device to the extraction tower 151.

[0089] The post-treatment unit 170 also includes: an alkali pump 176, an alkali solution pump 177, and an exhaust pump 178. The alkali pump 176 is connected to the inlet end of the alkali tower 171 and the concentrated alkali storage tank 175, respectively, to transport the concentrated alkali solution in the concentrated alkali storage tank 175 to the alkali tower 171. The alkali solution pump 177 is connected to the inlet end of the alkali solution settling tank 172 and the outlet end of the alkali tower 171, respectively, to transport the raffinate treated by the alkali tower 171 to the alkali solution settling tank 172. The exhaust pump 178 is connected to the outlet end of the third heat exchanger 180 and the alkali solution settling tank 172, respectively, to transport the waste gas generated by thermal decomposition in the alkali solution settling tank 172 to the third heat exchanger 180.

[0090] In some embodiments, the third heat exchanger 180 is connected to the outlet end of the alkali settler 172 and the fifth heat exchange pipeline 1443, respectively. The waste gas generated in the alkali settler 172 is transported to the third heat exchanger 180, and the waste gas has low-grade heat energy, so that heat exchange is completed in the third heat exchanger 180 to realize the recovery of low-grade heat energy.

[0091] Specifically, refer to Figure 1 The third heat exchanger 180 includes a first heat exchange section 181 and a second heat exchange section 182. The first heat exchange section 181 is provided with a first heat exchange channel 1811. The second heat exchange section 182 is provided within the first heat exchange channel 1811 and has a second heat exchange channel 1821. The first heat exchange channel 1811 is connected to the outlet end of the alkali settler 172 and the external atmospheric space, respectively. The second heat exchange channel 1821 is connected to the external water storage equipment and the fifth heat exchange pipeline 1443, respectively.

[0092] Understandably, the waste gas generated by thermal decomposition in the alkali settling tank 172 has low-grade heat energy. The waste gas generated in the alkali settling tank 172 is transported to the first heat exchange channel 1811 by the suction pump 178. Water in the external water storage device is transported to the second heat exchange channel 1821 to exchange heat with the waste gas in the first heat exchange channel 1811. After being heated in the second heat exchange channel 1821, the water is transported to the fifth heat exchange pipeline 1443 to exchange heat with the refrigerant water in the evaporation chamber 1442 to heat and evaporate the refrigerant water into steam. The waste gas after heat exchange is completed is discharged from the first heat exchange channel 1811 to further recover and reuse the low-grade heat energy, effectively avoiding heat loss and saving energy. This contributes to the energy saving and emission reduction of the hydrogen peroxide production device 100, giving the hydrogen peroxide production device 100 excellent energy-saving value.

[0093] In some embodiments, refer to Figure 1 The third heat exchanger 180 also includes a second water pump 183 and a third water pump 184. The second water pump 183 is connected to the second heat exchange channel 1821 and an external water storage device to transport water from the external water storage device to the second heat exchange channel 1821. The third water pump 184 is connected to the second heat exchange channel 1821 and the fifth heat exchange pipeline 1443 to transport the water that has completed heat exchange in the second heat exchange channel 1821 to the fifth heat exchange pipeline 1443.

[0094] In some embodiments, the inlet end of the fourth heat exchange pipeline 1433 may be connected to the regenerated liquid collector 174, and the outlet end of the fourth heat exchange pipeline 1433 may be connected to the regenerated liquid storage tank 112. The regenerated liquid prepared in the regenerated liquid collector 174 is transported to the fourth heat exchange pipeline 1433 for heat exchange and heating, and then transported to the regenerated liquid storage tank 112 for reuse, so as to realize the recovery and reuse of low-grade heat energy generated in the hydrogen peroxide production device 100.

[0095] In summary, referring to Figure 1 and Figure 3 The specific workflow of the hydrogen peroxide production device 100 in this application is as follows: Pure hydrogen in the external hydrogen storage equipment is compressed into hydrogen gas at a certain pressure by the hydrogen compressor 116 and then transported to the hydrogenation tower 111. The regenerated liquid in the regenerated liquid storage tank 112 is transported to the heater 113, and after being preheated to a certain temperature by the heater 113, it is transported to the hydrogenation tower 111. The hydrogen gas located in the hydrogenation tower 111 reacts with ethyl anthraquinone in the regenerated liquid to obtain hydrogenated liquid. The generated hydrogen... The hydrated liquid is transported to filter 114, and after being filtered by filter 114, it flows evenly into hydrogenated clay bed 115. It is then transported by hydrated liquid pump 117 to the first heat exchange pipeline 1321 of the first heat exchanger 130 to exchange heat with the water in the first heat exchange chamber 1311. The hydrated liquid is cooled, and the water in the first heat exchange chamber 1311 is heated. After the heat exchange is completed, the hydrated liquid is transported to oxidation tower 121, and the water in the first heat exchange chamber 1311 is transported to absorption heat pump unit 140.

[0096] After heat exchange, the hydrogenated liquid is transported to the oxidation tower 121, and the air is compressed by the air compressor 125 and then transported to the oxidation tower 121. The air and the hydrogenated liquid undergo an oxidation reaction at a set temperature and pressure to generate an oxidized liquid. The generated oxidized liquid is transported to the separator 122, where it is separated to complete gas-liquid separation. The tail gas obtained in the separator 122 is transported to the tail gas processor 123, where it is processed and then discharged into the air. The oxidized liquid after separating the tail gas is transported to the oxidized liquid storage tank 124, and then transported by the oxidized liquid pump 126 to the second heat exchange pipeline 1322 of the first heat exchanger 130 to exchange heat with the water in the first heat exchange chamber 1311. The oxidized liquid is cooled, and the water in the first heat exchange chamber 1311 is heated. After heat exchange, the oxidized liquid is transported to the extraction tower 151, and the water in the first heat exchange chamber 1311 is transported to the absorption heat pump unit 140.

[0097] Water from an external water storage device is transported to extraction tower 151, and the oxidized liquid after heat exchange is also transported to extraction tower 151. The oxidized liquid and water are contacted countercurrently in extraction tower 151 to complete extraction, yielding a hydrogen peroxide solution and raffinate of appropriate concentration. The hydrogen peroxide solution of appropriate concentration in extraction tower 151 is transported to purification tower 161, which contains a solvent oil column. The hydrogen peroxide solution settles to the bottom of purification tower 161 due to its density difference, allowing impurities to dissolve in the solvent. The purified hydrogen peroxide solution is then transported to hydrogen peroxide storage tank 162 for storage. The raffinate is transported to raffinate separator 152, and the raffinate after treatment in raffinate separator 152 is transported to alkali tower 171 for concentrated alkali. The concentrated alkali solution in storage 175 is conveyed to alkali tower 171, where it reacts with the raffinate to remove hydrogen peroxide. The raffinate treated in alkali tower 171 is then conveyed to alkali settling tank 172 for thermal decomposition. The waste gas generated by thermal decomposition is conveyed to the third heat exchanger 180. The raffinate in alkali settling tank 172, after dehydration and degassing, is conveyed to post-treatment clay bed 173. The raffinate is dehydrogenated in post-treatment clay bed 173 to generate ethyl anthraquinone. The ethyl anthraquinone obtained in post-treatment clay bed 173 is conveyed to regenerated liquid collector 174 to prepare regenerated liquid, which can then flow back into regenerated liquid storage 112 for later use.

[0098] The waste gas generated by thermal decomposition in the alkali settler 172 has low-grade heat energy. The waste gas generated in the alkali settler 172 is transported to the first heat exchange channel 1811 by the air pump 178. Water in the external water storage device is transported to the second heat exchange channel 1821 to exchange heat with the waste gas in the first heat exchange channel 1811. After being heated in the second heat exchange channel 1821, the water is transported to the fifth heat exchange pipeline 1443. The waste gas after heat exchange is completed is discharged from the first heat exchange channel 1811.

[0099] The water that has undergone heat exchange in the first heat exchange chamber 1311 is transported to the third heat exchange pipe 1413, and the dilute lithium bromide solution in the absorber 143 is transported to the first spray section 1414. The first spray section 1414 sprays the dilute lithium bromide solution into the first chamber 1412, so that the dilute lithium bromide solution comes into contact with the third heat exchange pipe 1413. The dilute lithium bromide solution exchanges heat with the water that has undergone heat exchange in the third heat exchange pipe 1413. After heating, the dilute lithium bromide solution is concentrated into a concentrated lithium bromide solution, and steam is generated. The steam is transported to the condenser 142, and the external condensate circulation equipment transports the condensate to the condenser pipe 1423. The steam comes into contact with the condenser pipe 1423, so that the steam and the condensate exchange heat. The steam is condensed into refrigerant water, which is transported to the third spray section 1414 of the evaporator 144. 44. The third spray section 1444 sprays refrigerant water into the evaporation chamber 1442 to contact the fifth heat exchange pipe 1443, so that the refrigerant water and the fluid with low-grade heat energy in the fifth heat exchange pipe 1443 can exchange heat. The refrigerant water is heated and evaporated into steam. The steam in the evaporator 144 is transported to the second chamber 1432 of the absorber 143. The heated lithium bromide concentrated solution is transported to the second spray section 1434 of the absorber 143. The second spray section 1434 sprays the lithium bromide concentrated solution into the second chamber 1432, so that the lithium bromide concentrated solution can contact the steam. The lithium bromide concentrated solution absorbs the steam to dilute into a lithium bromide dilute solution. At the same time, heat is released to heat the fluids to be heated in other production processes flowing in the fourth heat exchange pipe 1433, so as to ultimately realize the recovery and utilization of low-grade heat energy.

[0100] The above steps are provided only to help understand the method, structure, and core ideas of this application. Those skilled in the art can make various improvements and modifications to this application without departing from its principles, and these improvements and modifications also fall within the scope of protection of the claims.

Claims

1. A hydrogen peroxide production apparatus, characterized in that, include: Hydrogenation unit, oxidation unit, first heat exchanger and absorption heat pump unit; The first heat exchanger includes: a first heat exchange body and heat exchange pipelines. The first heat exchange body is provided with a first heat exchange cavity. At least a portion of the heat exchange pipelines are provided in the first heat exchange cavity. The hydrogenation unit and the oxidation unit are both connected to the heat exchange pipelines. The inlet end of the first heat exchange cavity is connected to an external water storage device, and the outlet end of the first heat exchange cavity is connected to the absorption heat pump unit.

2. The hydrogen peroxide production apparatus as described in claim 1, characterized in that, The heat exchange pipeline includes: a first heat exchange pipeline and a second heat exchange pipeline. At least a portion of the first heat exchange pipeline is disposed in the first heat exchange chamber. The inlet end of the first heat exchange pipeline is connected to the hydrogenation unit, and the outlet end of the first heat exchange pipeline is connected to the oxidation unit. At least a portion of the second heat exchange pipeline is disposed in the first heat exchange chamber, and the inlet end of the second heat exchange pipeline is connected to the oxidation unit.

3. The hydrogen peroxide production apparatus as described in claim 2, characterized in that, The absorption heat pump unit includes: a generator, a condenser, an absorber, and an evaporator. The generator is connected to the outlet end of the first heat exchange chamber, the condenser and the absorber respectively. The condenser is connected to the external condensate circulation equipment and the evaporator respectively. The absorber is connected to the evaporator. The generator contains a concentrated lithium bromide solution and the absorber contains a dilute lithium bromide solution.

4. The hydrogen peroxide production apparatus as described in claim 3, characterized in that, The generator includes: a generator body, a first cavity, the first cavity being connected to the absorber, and a concentrated lithium bromide solution stored in the first cavity; A third heat exchange pipeline, at least partially disposed within the first cavity, is connected to both the outlet end of the first heat exchange cavity and an external water storage device; and A first spray section is disposed within the first cavity, and the first spray section is connected to the absorber; The condenser includes: a condenser body with a condensation chamber connected to the first cavity and the evaporator; and a condensation pipe, at least a portion of which is located within the condensation chamber and connected to an external condensate circulation device.

5. The hydrogen peroxide production apparatus as described in claim 4, characterized in that, The absorber includes: an absorber body, a second cavity, the second cavity being connected to the first spray section, and a dilute lithium bromide solution stored in the second cavity; A fourth heat exchange conduit, at least partially disposed in the second cavity, is configured to allow flow of the fluid to be heated; and A second spray section is disposed in the second cavity, and the second spray section is connected to the first cavity; The evaporator includes: an evaporator body, which is provided with an evaporation chamber, and the evaporation chamber is connected to the second chamber; The fifth heat exchange pipeline, at least a portion of which is disposed within the evaporation chamber; and A third spray section is disposed in the evaporation chamber and is connected to the condensation chamber.

6. The hydrogen peroxide production apparatus as described in claim 5, characterized in that, The absorption heat pump unit further includes a second heat exchanger, which includes a second heat exchange shell and a sixth heat exchange pipeline. The second heat exchange shell is provided with a second heat exchange cavity, which is connected to the second cavity and the first spray section respectively. At least a portion of the sixth heat exchange pipeline is provided in the second heat exchange cavity, and the sixth heat exchange pipeline is connected to the first cavity and the second spray section respectively.

7. The hydrogen peroxide production apparatus as described in claim 5, characterized in that, Also includes: An extraction tower, the inlet of which is connected to the outlet of the second heat exchange pipeline and an external water storage device. A purification tower, wherein the inlet end of the purification tower is connected to the outlet end of the extraction tower; A hydrogen peroxide storage device is connected to the outlet end of the purification tower; An alkali tower, the inlet of which is connected to the outlet of the extraction tower and a concentrated alkali storage tank. An alkali settling device, wherein the inlet end of the alkali settling device is connected to the outlet end of the alkali tower; and The third heat exchanger is connected to the outlet end of the alkali sedimentation device and the fifth heat exchange pipeline.

8. The hydrogen peroxide production apparatus as described in claim 7, characterized in that, Also includes: A raffinate separator is connected to both the outlet of the extraction tower and the inlet of the alkali tower. A post-treatment white clay bed, wherein the post-treatment white clay bed is connected to the outlet end of the alkaline sedimentation device; The regenerated liquid collector is connected to the post-treatment clay bed.

9. The hydrogen peroxide production apparatus as described in claim 7, characterized in that, The third heat exchanger includes: a first heat exchange section and a second heat exchange section. The first heat exchange section is provided with a first heat exchange channel. The second heat exchange section is disposed within the first heat exchange channel and is provided with a second heat exchange channel. The first heat exchange channel is connected to the outlet end of the alkali sedimentation device and the external atmospheric space, respectively. The second heat exchange channel is connected to the external water storage device and the fifth heat exchange pipeline, respectively.

10. The hydrogen peroxide production apparatus as described in claim 2, characterized in that, The hydrogenation unit includes: a hydrogenation tower, a regenerated liquid storage tank, a heater, a filter, and a hydrogenated clay bed. The inlet end of the hydrogenation tower is connected to an external hydrogen storage device. The regenerated liquid storage tank is connected to the inlet end of the hydrogenation tower through the heater. The filter is connected to the outlet end of the hydrogenation tower and the hydrogenated clay bed, respectively. The hydrogenated clay bed is connected to the inlet end of the first heat exchange pipeline. The oxidation unit includes an oxidation tower, a separator, an exhaust gas processor, and an oxidation liquid storage tank. The inlet end of the oxidation tower is connected to the outlet end of the first heat exchange pipeline and the external atmospheric space, respectively. The outlet end of the oxidation tower is connected to the inlet end of the separator. The outlet end of the separator is connected to the exhaust gas processor and the oxidation liquid storage tank, respectively. The oxidation liquid storage tank is also connected to the inlet end of the second heat exchange pipeline.

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