Continuous production device suitable for various hydroxime extraction agents
By designing a continuous production unit suitable for hydroxyoxime extractants, the problem of intermittent post-processing in the production of hydroxyoxime extractants was solved, realizing fully continuous production from raw materials to finished products, and improving production efficiency and product quality.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- CHONGQING KOOPPER CHEM IND
- Filing Date
- 2025-05-21
- Publication Date
- 2026-05-08
AI Technical Summary
The existing production process for hydroxyoxime extractants suffers from intermittent post-processing, resulting in long production cycles and an inability to meet market demand.
A continuous production device suitable for various hydroxyoxime extractants was designed, including a continuous feeding unit, a microchannel reaction unit, a continuous phase separation unit, a continuous distillation unit, a continuous decolorization unit, a continuous water washing unit, and a continuous dehydration unit, realizing fully continuous production from raw materials to finished products.
It enables fully continuous production of hydroxyoxime extractants, shortens reaction and post-processing time, improves production efficiency, reduces side reactions, and is applicable to the production of various hydroxyoxime extractants.
Smart Images
Figure CN224207993U_ABST
Abstract
Description
Technical Field
[0001] This utility model belongs to the field of chemical equipment technology, specifically relating to a continuous production device suitable for various hydroxyoxime extractants. Background Technology
[0002] Hydroxyoxime extractants exhibit good selectivity for copper, preferentially extracting copper from multiple elements, and are widely used in the copper extraction industry. The industrial synthesis of hydroxyoxime extractants often employs a batch oximation reaction in a batch reactor. This reaction involves the neutralization of hydroxylamine salts (hydrochloride or sulfate) with an alkali (organic or inorganic base) to release free hydroxylamine, which then reacts with aldehyde / ketone substrates to form oximes. This process is time-consuming, and subsequent processing is time-consuming, resulting in low equipment utilization, long production cycles, and low capacity, failing to meet the growing market demand.
[0003] Microchannel continuous flow reaction is characterized by safety, stability, and a high degree of automation. Compared to conventional batch reactions, it uses a pump as the power source for the reaction flow, delivering materials into the reaction channel and confining the chemical reaction to a very small area. This enhances the efficient mixing of reactants, allowing the chemical reaction to occur under continuous flow conditions. The greatest advantage of continuous flow reaction systems compared to batch reactions is their superior surface area to volume ratio. This allows for efficient heat and mass transfer, resulting in advantages such as a large reaction contact area, high heat and mass transfer efficiency, short reaction residence time, low probability of side reactions, high conversion rate, low risk factor, and scalability for large-scale production. Therefore, a microchannel continuous synthesis process suitable for hydroxyoxime extractants can be developed.
[0004] However, current focus in continuous synthesis processes is often concentrated on the microchannel continuous flow reaction section, while less attention is paid to the post-processing section. Furthermore, post-processing processes often vary significantly depending on the reaction, resulting in a situation where the reaction section is continuous while the post-processing section is intermittent. To address this, it is necessary to design a fully continuous system that includes both the reaction and post-processing sections, thereby truly achieving continuous production of hydroxyoxime extractants from raw materials to finished products. Utility Model Content
[0005] The present invention aims to provide a continuous production apparatus suitable for various hydroxyoxime extractants, in order to solve the problem of intermittent post-processing in microchannel continuous synthesis processes.
[0006] To achieve the above objectives, the present invention provides a continuous production apparatus suitable for various hydroxyoxime extractants, comprising a continuous feeding unit and a microchannel reaction unit, and further comprising a continuous phase separation unit, a continuous distillation unit, a continuous decolorization unit, a continuous washing unit, a continuous dehydration unit, and a finished product tank connected in sequence. The outlet of the microchannel reaction unit is connected to the inlet of the continuous phase separation unit, the inlet of the continuous distillation unit, and the inlet of the continuous decolorization unit via pipelines. Valves are provided on the pipelines between the outlet of the continuous phase separation unit and the inlet of the continuous distillation unit, between the outlet of the continuous distillation unit and the inlet of the continuous decolorization unit, and on the pipelines.
[0007] The working principle and beneficial effects of this scheme are as follows: This scheme divides the post-processing section of the microchannel continuous synthesis process into a continuous phase separation module, a continuous distillation module, a continuous decolorization module, a continuous water washing module, and a continuous dehydration module, achieving full continuity in the post-processing section. Furthermore, the microchannel reaction unit is directly connected to the continuous phase separation module, continuous distillation module, and continuous decolorization module. Thus, producers can select the initial post-processing step of the crude product from phase separation, distillation, and decolorization according to the actual post-processing requirements of the crude product, thereby choosing whether to perform phase separation, distillation, and decolorization treatments on the crude product. This approach is suitable for the continuous synthesis of various hydroxyoxime extractants and is suitable for widespread application.
[0008] Optionally, the outlet of the microchannel reaction unit is connected to the inlet of the continuous washing unit and the finished product tank via pipes, and a valve is provided between the outlet of the continuous decolorization unit and the inlet of the continuous washing unit.
[0009] In this scheme, the microchannel reaction unit is directly connected to the continuous water washing module and the finished product tank. Thus, the initial post-treatment of the crude product can be selected from phase separation, distillation, decolorization and water washing, or it can be directly put into the finished product tank for storage without post-treatment, which provides more diverse options.
[0010] Optionally, the outlet of the continuous phase separation unit is connected to the inlet of the continuous decolorization unit, and a valve is provided between the outlet of the continuous phase separation unit and the inlet of the continuous decolorization unit.
[0011] In this scheme, after the continuous phase separation unit is connected to the continuous decolorization unit, the crude product can be decolorized directly after phase separation. That is, the post-processing steps of the crude product can be phase separation-decolorization-water washing-dehydration, which is suitable for crude products that do not require distillation, such as ketoxime products.
[0012] Optionally, the outlet of the continuous phase separation unit is connected to the inlet of the continuous water washing unit, and a valve is provided between the outlet of the continuous phase separation unit and the inlet of the continuous water washing unit.
[0013] In this scheme, the crude product obtained by the microchannel reaction unit can be processed in a post-treatment sequence of phase separation-water washing-dehydration to obtain the finished product, and the choice of post-treatment process is more diversified.
[0014] Optionally, the outlet of the continuous distillation unit is connected to the inlet of the continuous water washing unit, and a valve is provided between the outlet of the continuous distillation unit and the inlet of the continuous water washing unit.
[0015] In this scheme, the crude product obtained through the microchannel reaction unit can be processed in a sequence of distillation-washing-dehydration to obtain the finished product, thus allowing for a more diverse range of post-processing steps.
[0016] Optionally, the continuous phase separation unit includes a centrifugal extractor and a membrane separator, wherein the light phase outlet of the centrifugal extractor is connected to the feed inlet of the continuous distillation unit, and the heavy phase outlet of the centrifugal extractor is connected to the feed inlet of the membrane separator.
[0017] In this scheme, a centrifugal extractor is used to achieve continuous phase separation, resulting in a continuous light phase and a continuous heavy phase, so that the light phase (containing the target product) can continuously enter the next post-processing step; and a membrane separator is used to recover water and raw material diluent from the heavy phase.
[0018] Optionally, the continuous distillation unit includes a distillation column I, a tubular reactor I, and a finished product diluent storage tank. The bottom product of the distillation column I and the finished product diluent in the finished product diluent storage tank are both transported to the tubular reactor I. The outlet of the tubular reactor I is connected to the inlet of the continuous decolorization unit.
[0019] In this scheme, continuous distillation of the product is achieved using distillation column I, and the distilled product (including the target product) is mixed with the finished product diluent in tubular reactor I to improve the product's fluidity so that it can better enter the next post-processing step.
[0020] Optionally, the continuous decolorization unit includes a sulfuric acid storage tank and a tubular reactor II. The sulfuric acid in the sulfuric acid storage tank and the output from the tubular reactor I are both transported to the tubular reactor II. The outlet of the tubular reactor II is connected to the inlet of the continuous water washing unit.
[0021] In this scheme, sulfuric acid and the product from the previous post-processing step are fed into tubular reactor II together, thereby achieving continuous decolorization of the product.
[0022] Optionally, the continuous washing unit includes a four-stage countercurrent centrifugal extractor.
[0023] In this scheme, four centrifugal extractors connected in series are used to achieve continuous water washing of the product, thereby washing away the sulfuric acid.
[0024] Optionally, the continuous dehydration unit includes a distillation column II, the bottom outlet of which is connected to the finished product tank.
[0025] In this scheme, distillation column II is used to continuously dehydrate the product, thereby obtaining the finished product, which is then sent to the finished product tank for storage. Attached Figure Description
[0026] Figure 1 This is a schematic diagram of the continuous production apparatus for various hydroxyoxime extractants in Embodiment 1 of this utility model;
[0027] Figure 2 This is a schematic diagram of the continuous production apparatus for various hydroxyoxime extractants in Embodiment 2 of this utility model;
[0028] Figure 3 This is a schematic diagram of the continuous production apparatus for various hydroxyoxime extractants in Embodiment 3 of this utility model;
[0029] Figure 4 This is a schematic diagram of the continuous production apparatus for various hydroxyoxime extractants in Embodiment 4 of this utility model;
[0030] Figure 5 This is a schematic diagram of the continuous production apparatus for various hydroxyoxime extractants in Embodiment 5 of this utility model. Detailed Implementation
[0031] The following detailed description illustrates the specific implementation method:
[0032] The markings in the accompanying drawings include: continuous feeding unit 100, mixing tank I 101, mixing tank II 102, powder storage bin I 103, powder temporary storage bin I 104, powder storage bin II 105, powder temporary storage bin II 106, negative pressure system 107, water storage tank 108, microchannel reaction unit 200, microchannel reactor 201, continuous phase separation unit 300, centrifugal extractor 301, membrane separator 302, water collector 303, raw material diluent collector 304, continuous... Distillation unit 400, distillation column I 401, tubular reactor I 402, finished product diluent storage tank 403, raw material diluent recovery tank 404, continuous decolorization unit 500, sulfuric acid storage tank 501, tubular reactor II 502, continuous water washing unit 600, four-stage countercurrent centrifugal extractor 601, continuous dehydration unit 700, distillation column II 701, water recovery tank 702, finished product tank 8, valve 9, transfer pump 10, bypass pipe I 11, bypass pipe II 12, bypass pipe III 13.
[0033] Example 1
[0034] This embodiment is basically as follows: Figure 1As shown: A continuous production apparatus suitable for various hydroxyoxime extractants, including a continuous feeding unit 100, a microchannel reaction unit 200, and sequentially connected continuous phase separation unit 300, continuous distillation unit 400, continuous decolorization unit 500, continuous water washing unit 600, continuous dehydration unit 700, and finished product tank 8.
[0035] The continuous feeding unit 100 includes a stirred tank I 101 and a stirred tank II 102. Stirred tank I 101 stores free hydroxylamine released from hydroxylamine salt after neutralization with alkali, and stirred tank II 102 stores aldehydes / ketones. Specifically, under stirring conditions, water, hydroxylamine salt, and caustic alkali are added to stirred tank I 101 to obtain a mixed hydroxylamine solution containing free hydroxylamine; under stirring conditions, a raw material diluent and an aldehyde / ketone are added to stirred tank II 102 to obtain a mixed solution of aldehyde / ketone and raw material diluent.
[0036] The microchannel reaction unit 200 includes several microchannel reactors 201 connected in series. The first microchannel reactor 201 has two feed ports. Liquid raw materials in the stirred tank I 101 and stirred tank II 102 enter the microchannel reactor 201 through the two feed ports respectively.
[0037] The continuous phase separation unit 300 includes a centrifugal extractor 301 and a membrane separator 302. The outlet of the microchannel reactor 201 located at the tail end is connected to the two-phase feed inlet of the centrifugal extractor 301. The heavy phase outlet of the centrifugal extractor 301 is connected to the feed inlet of the membrane separator 302. After separation by the membrane separator 302, water enters the water collector 303, and the raw material diluent enters the raw material diluent collector 304.
[0038] The continuous distillation unit 400 includes a distillation column I 401, a tubular reactor I 402, a finished product diluent storage tank 403, and a raw material diluent recovery tank 404. The light phase outlet of the centrifugal extractor 301 is connected to the feed inlet of the distillation column I 401. The bottom product of the distillation column I 401 and the finished product diluent in the finished product diluent storage tank 403 are both transported to the tubular reactor I 402. The top product of the distillation column I 401 enters the raw material diluent recovery tank 404.
[0039] The continuous decolorization unit 500 includes a sulfuric acid storage tank 501 and a tubular reactor II 502. The sulfuric acid aqueous solution in the sulfuric acid storage tank 501 and the discharge from the tubular reactor I 402 are both transported to the tubular reactor II 502.
[0040] The continuous washing unit 600 includes a four-stage countercurrent centrifugal extractor 601, and the outlet of the tubular reactor II 502 is connected to the first-stage biphase feed inlet of the four-stage countercurrent centrifugal extractor 601.
[0041] The continuous dehydration unit 700 includes a distillation column II 701 and a water recovery tank 702. The feed inlet of the distillation column II 701 is connected to the fourth-stage light phase outlet of the four-stage countercurrent centrifugal extractor 601. The bottom outlet of the distillation column II 701 is connected to the finished product tank 8. The top of the distillation column II 701 is discharged into the water recovery tank 702.
[0042] The outlet of the microchannel reaction unit 200 is connected to the inlet of the continuous phase separation unit 300, the inlet of the continuous distillation unit 400, the inlet of the continuous decolorization unit 500, the inlet of the continuous water washing unit 600, and the finished product tank 8, respectively. Furthermore, valves 9 are installed between the microchannel reaction unit 200 and the continuous phase separation unit 300, between the microchannel reaction unit 200 and the continuous distillation unit 400, between the microchannel reaction unit 200 and the continuous decolorization unit 500, between the microchannel reaction unit 200 and the continuous water washing unit 600, between the microchannel reaction unit 200 and the finished product tank 8, between the continuous phase separation unit 300 and the continuous distillation unit 400, between the continuous distillation unit 400 and the continuous decolorization unit 500, and between the continuous decolorization unit 500 and the continuous water washing unit 600 to control the on / off state of the pipelines. In addition, liquid transportation in the entire device is achieved through a transfer pump 10 (some transfer pumps 10 are not shown in the figure).
[0043] This embodiment uses the production of 2-hydroxy-5-nonylbenzaldehyde oxime as an example for detailed explanation. During use, valves 9 between the microchannel reaction unit 200 and the continuous phase separation unit 300, between the continuous phase separation unit 300 and the continuous distillation unit 400, between the continuous distillation unit 400 and the continuous decolorization unit 500, and between the continuous decolorization unit 500 and the continuous water washing unit 600 are all open. Valves 9 between the microchannel reaction unit 200 and the continuous distillation unit 400, between the microchannel reaction unit 200 and the continuous decolorization unit 500, between the microchannel reaction unit 200 and the continuous water washing unit 600, and between the microchannel reaction unit 200 and the finished product tank 8 are closed.
[0044] During production, water enters mixing tank I101, and stirring is started. Hydroxylamine sulfate is then added to mixing tank I101 to prepare a hydroxylamine sulfate solution of the required concentration. Sodium hydroxide is then added to mixing tank I101 to prepare a sodium hydroxide solution of the required concentration. The hydroxylamine sulfate solution and the sodium hydroxide solution are thoroughly mixed to obtain a mixed hydroxylamine solution. 2-Hydroxy-5-nonylbenzaldehyde and tert-butanol (raw material diluent) are then added to mixing tank II102, and stirring is started to obtain a mixed solution of 2-hydroxy-5-nonylbenzaldehyde and tert-butanol of the required concentration.
[0045] Under the pumping of the corresponding transfer pump 10, the mixed hydroxylamine solution in stirred tank I 101 and the mixed tert-butanol solution in stirred tank II 102 enter the microchannel reactor 201 through two feed ports, respectively. The reaction temperature is controlled at 80±3℃ (internal temperature), and the reaction time is controlled within 0.5h. A two-phase crude product (aqueous phase and organic phase) is obtained from the outlet of the microchannel reactor 201 located at the tail end. The upper organic phase contains crude 2-hydroxy-5-nonylbenzaldehyde oxime and tert-butanol, and is brown in color. The lower aqueous phase contains sodium sulfate, water, and a small amount of tert-butanol.
[0046] The crude biphase product is fed to the biphase feed port at the bottom of the centrifugal extractor 301. After phase separation by the centrifugal extractor 301, the light phase (upper organic phase) enters the distillation column I 401, and the heavy phase (lower aqueous phase) enters the membrane separator 302 to separate water and tert-butanol. The water enters the water collector 303 for subsequent water treatment, and the tert-butanol enters the raw material diluent collector 304 for subsequent recovery and reuse.
[0047] Distillation column I 401 separates the crude 2-hydroxy-5-nonylbenzaldehyde oxime and tert-butanol from the light phase. The tert-butanol enters the feed diluent recovery tank 404 for subsequent recycling. The crude 2-hydroxy-5-nonylbenzaldehyde oxime, along with the finished product diluent (kerosene), is thoroughly mixed in tubular reactor I 402 and then pumped to tubular reactor II 502 by the corresponding transfer pump 10. Simultaneously, a 12.7 wt% dilute sulfuric acid aqueous solution is pumped to tubular reactor II 502 by the corresponding transfer pump 10. The dilute sulfuric acid aqueous solution, crude 2-hydroxy-5-nonylbenzaldehyde oxime, and finished product diluent are thoroughly mixed and reacted in tubular reactor II 502 at a reaction temperature controlled at 65 ± 3 °C. A two-phase product is obtained at the outlet of tubular reactor II 502: the upper organic phase is decolorized 2-hydroxy-5-nonylbenzaldehyde oxime, which is yellow in color, and the lower phase is an aqueous phase.
[0048] Then, the above-mentioned biphase product is fed into a four-stage countercurrent centrifugal extractor 601. The first stage separates the acid water, and water is fed into the inlet of the second, third and fourth stage heavy phases at a rate of 50 g / min for continuous water washing of the biphase product. Finally, the 2-hydroxy-5-nonylbenzaldehyde oxime product containing only a small amount of water flows out from the outlet of the fourth stage light phase.
[0049] Finally, the above-mentioned 2-hydroxy-5-nonylbenzaldehyde oxime product is transported to distillation column II 701 to separate water and 2-hydroxy-5-nonylbenzaldehyde oxime. The water enters the water recovery tank 702, while the 2-hydroxy-5-nonylbenzaldehyde oxime enters the finished product tank 8 for storage.
[0050] Thus, the continuous synthesis of 2-hydroxy-5-nonylbenzaldehyde oxime is achieved. Compared with batch synthesis processes, this embodiment significantly shortens the reaction time and post-processing time, realizing a fully continuous process from raw materials to the final product. Furthermore, no other byproducts are produced during the reaction except for sodium sulfate; the solvent water and the raw material diluent tert-butanol can be reused, and the recovery efficiency of tert-butanol is high, making it environmentally friendly.
[0051] In addition, in this embodiment, the two-phase crude product at the outlet of the microchannel reactor 201 can be directly fed into the continuous phase separation unit 300, the continuous distillation unit 400, the continuous decolorization unit 500, the continuous water washing unit 600, or the finished product tank 8 by controlling the valve 9. Thus, a suitable post-processing procedure can be selected according to the actual post-processing requirements of the crude product, which is suitable for the continuous synthesis of various hydroxyoxime extractants. Specifically, in this embodiment, under the control of valve 9, the crude product at the outlet of microchannel reactor 201 can undergo the following optional post-processing steps: 1) phase separation-distillation-decolorization-washing-dehydration (suitable for aldoxime processes); 2) distillation-decolorization-washing-dehydration (suitable for homogeneous reaction types where the raw material contains a refining diluent); 3) decolorization-washing-dehydration (suitable for homogeneous reaction types where the raw material does not contain a refining diluent, and the reaction type requires salt washing); 4) washing-dehydration (suitable for homogeneous reaction types where the raw material does not contain a refining diluent, and the reaction type does not require decolorization but requires salt washing); 5) no post-processing is required, and the crude product directly enters the finished product tank 8.
[0052] Example 2
[0053] The difference between this embodiment and Embodiment 1 is that: Figure 2 As shown, in this embodiment, the outlet of the continuous phase separation unit 300 and the inlet of the continuous decolorization unit 500 are connected by a crossover pipe I11, and a valve 9 for controlling its on / off state is provided on the crossover pipe I11.
[0054] In this embodiment, valve 9 on the crossover pipe I11 is opened, connecting the outlet of the continuous phase separation unit 300 with the inlet of the continuous decolorization unit 500. Simultaneously, valve 9 near the inlet and outlet of the continuous distillation unit 400 is closed, thereby severing the connection between the continuous phase separation unit 300 and the continuous distillation unit 400, as well as the connection between the continuous distillation unit 400 and the continuous decolorization unit 500. Thus, the light phase discharged from the light phase outlet of the centrifugal extractor 301 is transported to the continuous decolorization unit 500 via the crossover pipe I11, allowing for four post-processing steps of phase separation, decolorization, water washing, and dehydration of the biphasic crude product, eliminating the need for distillation. For example, when the product is 2-hydroxy-5-nonylacetophenone oxime, the biphasic crude product undergoes a "phase separation-decolorization-water washing-dehydration" post-processing step, suitable for ketoxime synthesis processes.
[0055] Example 3
[0056] The difference between this embodiment and Embodiment 2 is that: Figure 3 As shown, in this embodiment, the discharge port of the continuous phase separation unit 300 is connected to the continuous water washing unit 600 through a crossover pipe II 12, and a valve 9 for controlling its on / off state is provided on the crossover pipe II 12.
[0057] In this embodiment, valve 9 on the crossover pipe II 12 is opened, connecting the outlet of the continuous phase separation unit 300 with the continuous water washing unit 600. Simultaneously, valve 9 is closed between the outlet of the continuous phase separation unit 300 and the inlet of the continuous distillation unit 400, and also between the outlet of the continuous decolorization unit 500 and the inlet of the continuous water washing unit 600, thereby severing the connection between the continuous phase separation unit 300 and the continuous distillation unit 400, and between the continuous decolorization unit 500 and the continuous water washing unit 600. Thus, the crude product can be processed using a "phase separation-water washing-dehydration" post-treatment process, suitable for heterogeneous reaction types where the raw material does not contain a refining diluent, and reaction types that do not require decolorization but require salt washing.
[0058] Example 4
[0059] The only difference between this embodiment and Embodiment 3 is that: Figure 4 As shown, in this embodiment, the outlet of the continuous distillation unit 400 and the inlet of the continuous water washing unit 600 are connected by a crossover pipe III13, and a valve 9 for controlling its opening and closing is provided on the crossover pipe III13.
[0060] In this embodiment, valve 9 connects the microchannel reaction unit 200 and the continuous distillation unit 400 via the outlet of the microchannel reaction unit 200; valve 9 on the crossover pipe III 13 is opened to connect the outlet of the continuous distillation unit 400 and the inlet of the continuous washing unit 600; simultaneously, valve 9 is closed between the outlet of the microchannel reaction unit 200 and the inlet of the continuous phase separation unit 300 to disconnect the connection between the microchannel reaction unit 200 and the continuous phase separation unit 300; valve 9 is closed between the outlet of the continuous phase separation unit 300 and the inlet of the continuous distillation unit 400 to disconnect the connection between the continuous phase separation unit 300 and the continuous distillation unit 400; valve 9 is closed between the outlet of the continuous decolorization unit 500 and the continuous washing unit 600 to disconnect the connection between the continuous decolorization unit 500 and the continuous washing unit 600. Thus, the crude product from the microchannel reaction unit 200 directly enters the continuous distillation unit 400. The distilled product then enters the continuous water washing unit 600 via the bypass pipe III 13. After water washing, the product then enters the continuous dehydration unit 700. The dehydrated product is then stored in the finished product tank. That is, in this embodiment, by controlling the valve 9, the crude product can be selected to undergo a post-processing step of "distillation-water washing-dehydration," which is suitable for homogeneous reaction types where the raw material contains a refining diluent, and reaction types that do not require decolorization but require salt washing.
[0061] Example 5
[0062] The difference between this embodiment and Embodiment 1 is that: Figure 5As shown, in this embodiment, the continuous feeding unit 100 further includes a powder storage bin I 103, a powder temporary storage bin I 104, a powder storage bin II 105, a powder temporary storage bin II 106, a negative pressure system 107, and a water storage tank 108. Powder storage bins I 103, I 104, II 105, and II 106 are all connected to the negative pressure system 107. One end of powder temporary storage bin I 104 is connected to powder storage bin I 103, and the other end is connected to the mixing tank I 101. One end of powder temporary storage bin II 106 is connected to powder storage bin II 105, and the other end is connected to the mixing tank I 101. Powder storage bin I 103 is used to store hydroxylamine sulfate powder, and powder storage bin II 105 is used to store sodium hydroxide powder. Thus, in this embodiment, water enters the mixing tank I 101 under the pumping of the corresponding delivery pump 10; hydroxylamine sulfate powder enters the powder storage silo I 103 through the feeding port of the powder storage silo I 103, and then enters the mixing tank I 101 through the powder temporary storage silo I 104. During this process, the negative pressure system 107 provides negative pressure to prevent the powder from being difficult to enter; similarly, sodium hydroxide powder enters the powder storage silo II 105 through the feeding port of the powder storage silo II 105, and then enters the mixing tank I 101 through the powder temporary storage silo II 106. During this process, the negative pressure system 107 provides negative pressure, thereby realizing the automatic feeding of hydroxylamine sulfate powder and sodium hydroxide powder into the mixing tank I 101.
[0063] The above descriptions are merely embodiments of this utility model, and common knowledge regarding specific structures and characteristics is not elaborated upon here. It should be noted that those skilled in the art can make various modifications and improvements without departing from the structure of this utility model, and these should also be considered within the scope of protection of this utility model. These modifications will not affect the effectiveness or practicality of this utility model. The specific embodiments described in the specification can be used to interpret the claims.
Claims
1. A continuous production apparatus suitable for various hydroxyoxime extractants, comprising a continuous feeding unit and a microchannel reaction unit, characterized in that: It also includes a continuous phase separation unit, a continuous distillation unit, a continuous decolorization unit, a continuous washing unit, a continuous dehydration unit, and a finished product tank connected in sequence. The outlet of the microchannel reaction unit is connected to the inlet of the continuous phase separation unit, the inlet of the continuous distillation unit, and the inlet of the continuous decolorization unit through pipelines. Valves are provided on the pipelines between the outlet of the continuous phase separation unit and the inlet of the continuous distillation unit, between the outlet of the continuous distillation unit and the inlet of the continuous decolorization unit, and between the outlet of the continuous distillation unit and the inlet of the continuous decolorization unit.
2. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The outlet of the microchannel reaction unit is connected to the inlet of the continuous washing unit and the finished product tank via pipes. A valve is provided between the outlet of the continuous decolorization unit and the inlet of the continuous washing unit.
3. The continuous production apparatus for various hydroxyoxime extractants according to claim 2, characterized in that: The outlet of the continuous phase separation unit is connected to the inlet of the continuous decolorization unit, and a valve is provided between the outlet of the continuous phase separation unit and the inlet of the continuous decolorization unit.
4. The continuous production apparatus for various hydroxyoxime extractants according to claim 3, characterized in that: The outlet of the continuous phase separation unit is connected to the inlet of the continuous water washing unit, and a valve is provided between the outlet of the continuous phase separation unit and the inlet of the continuous water washing unit.
5. The continuous production apparatus for various hydroxyoxime extractants according to claim 1 or 4, characterized in that: The outlet of the continuous distillation unit is connected to the inlet of the continuous water washing unit, and a valve is provided between the outlet of the continuous distillation unit and the inlet of the continuous water washing unit.
6. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The continuous phase separation unit includes a centrifugal extractor and a membrane separator. The light phase outlet of the centrifugal extractor is connected to the feed inlet of the continuous distillation unit, and the heavy phase outlet of the centrifugal extractor is connected to the feed inlet of the membrane separator.
7. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The continuous distillation unit includes a distillation column I, a tubular reactor I, and a finished product diluent storage tank. The bottom product of the distillation column I and the finished product diluent in the finished product diluent storage tank are both transported to the tubular reactor I. The outlet of the tubular reactor I is connected to the inlet of the continuous decolorization unit.
8. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The continuous decolorization unit includes a sulfuric acid storage tank and a tubular reactor II. The sulfuric acid in the sulfuric acid storage tank and the output from the tubular reactor I are both transported to the tubular reactor II. The outlet of the tubular reactor II is connected to the inlet of the continuous water washing unit.
9. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The continuous washing unit includes a four-stage countercurrent centrifugal extractor.
10. The continuous production apparatus for various hydroxyoxime extractants according to claim 1, characterized in that: The continuous dehydration unit includes distillation column II, and the bottom outlet of distillation column II is connected to the finished product tank.