Physical field enhanced waste oil pretreatment apparatus and method

Abstract

The application discloses a kind of physical field reinforced waste oil pretreatment device and method.The device includes sequentially connected waste oil input unit, supergravity dynamic membrane type reaction unit, physical field coupling unit and dynamic tubular reaction unit;Waste oil input unit includes solid-liquid separator;Supergravity dynamic membrane type reaction unit includes supergravity dynamic membrane type reactor, and the input device of demulsifier, purified water and demetalizing agent is connected with its inlet respectively;Physical field coupling unit includes the coupling reactor of external applied physical field and the input device of sodium hydroxide solution is connected with its inlet;Dynamic tubular reaction unit includes dynamic tubular reactor and the input device of hydrogen peroxide is connected with its inlet, and the input device of demetalizing agent is also connected with the inlet of dynamic tubular reactor, and the outlet of coupling reactor and the outlet of dynamic tubular reactor are respectively provided with centrifugal separator between the inlet of dynamic tubular reactor.The device is more thorough to waste oil metal ion and other impurities removal.

Description

Technical Field

[0001] This invention relates to the fields of environmental protection and resource recycling technology, and in particular to a physical field-enhanced waste oil pretreatment device and method. Background Technology

[0002] Waste oil is one of the main raw materials for biofuels, but it has high acid value, many impurities, and complex composition. In particular, waste oil usually contains water, salt, and solid impurities. High phosphorus and high chlorine content can be toxic to hydrogenation catalysts, necessitating pretreatment to meet the feed conditions for hydrogenation and ensure long-term stable operation of the unit. Chinese patent CN 103571630 A discloses a pretreatment process for biodiesel production. This process involves adding acid and water, heating and mixing, allowing it to stand, precipitate, and separate the liquids, extracting the upper layer of oil, filtering to remove residue, adding concentrated acid and heating to carbonize and polymerize impurities, which then precipitate and separate. The acidified oil is then washed, dehydrated, and decolorized to obtain refined waste oil. While this method produces waste oil with low water and impurity content and uniform quality, it has poor metal ion removal efficiency, significantly shortening the catalyst life in the subsequent hydrogenation reaction. Furthermore, due to the complexity of the waste oil, precise control of the three-phase separation during the acidification, sedimentation, and separation steps is difficult, affecting subsequent extraction and processing efficiency. Chinese patent CN116355690 A discloses a pretreatment process for biodiesel feedstock. This process involves mixing acidified oil and waste animal and vegetable oils from the catering industry in different proportions according to pre-tested indicators. The mixture then undergoes preheating, a first water wash, a first centrifugation, a second water wash, a second centrifugation, alkali refining, a third centrifugation, a third water wash, a fourth centrifugation, a fourth water wash, a fifth centrifugation, drying, decolorization, filtration, deodorization, and cooling to obtain the finished oil. This method can effectively reduce the nitrogen, phosphorus, sulfur, and heavy metal content in waste oils (by removing impurities). However, the process requires four water washes and five centrifugations, making the process cumbersome, complex, and energy-intensive, increasing production costs and the difficulty of equipment maintenance and management. Furthermore, the centrifugation process generates a significant amount of wastewater, increasing the burden on wastewater treatment.

[0003] Therefore, in order to improve the removal rate and efficiency of impurities such as metal ions in waste oils, and to pretreat oils economically and efficiently so that they meet the requirements for subsequent hydrogenation reactions to produce biodiesel, there is an urgent need for an efficient and convenient waste oil pretreatment method. Summary of the Invention

[0004] In order to at least partially solve the technical problems existing in the prior art, the present invention proposes a physical field enhanced waste oil pretreatment device and method, which can thoroughly remove impurities such as metal ions in waste oil, and the treatment process is efficient and convenient.

[0005] In a first aspect, embodiments of the present invention provide a waste oil pretreatment device enhanced by physical field, comprising a waste oil input unit, a hypergravity dynamic membrane reaction unit, a physical field coupling unit, and a dynamic tubular reaction unit connected in sequence.

[0006] The waste oil input unit includes a waste oil input device and a solid-liquid separator;

[0007] The supergravity dynamic membrane reaction unit includes a supergravity dynamic membrane reactor and a demulsifier input device, a purified water input device, and a demetallizer input device respectively connected to its inlet.

[0008] The organic phase outlet of the solid-liquid separator is connected to the inlet of the ultragravity dynamic membrane reactor;

[0009] The physical field coupling unit includes a coupling reactor to which an external physical field is applied and a sodium hydroxide solution input device connected to its inlet;

[0010] The dynamic tubular reaction unit includes a dynamic tubular reactor and a hydrogen peroxide input device connected to its inlet. The demetallizing agent input device is also connected to the inlet of the dynamic tubular reactor. A first centrifugal separator is connected between the outlet of the coupled reactor and the inlet of the dynamic tubular reactor. A second centrifugal separator is connected to the outlet of the dynamic tubular reactor.

[0011] Optionally, a first flow control valve is installed on the pipeline connecting the waste oil input device and the inlet of the solid-liquid separator.

[0012] The solid outlet of the solid-liquid separator is connected to a solid collection device.

[0013] Optionally, a second flow control valve is installed on the pipeline connecting the demulsifier input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of the demulsifier input to the hypergravity dynamic membrane reactor.

[0014] A third flow control valve is installed on the pipeline connecting the purified water input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of purified water input to the hypergravity dynamic membrane reactor.

[0015] A fourth flow control valve is installed on the pipeline connecting the demetallizing agent input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of the demetallizing agent input to the hypergravity dynamic membrane reactor.

[0016] A fifth flow control valve is installed on the pipeline connecting the demetallizing agent input device and the inlet of the dynamic tubular reactor to control the flow rate of the demetallizing agent input to the dynamic tubular reactor;

[0017] A sixth flow control valve is installed on the pipeline connecting the hydrogen peroxide input device and the inlet of the dynamic tubular reactor to control the flow rate of hydrogen peroxide input to the dynamic tubular reactor.

[0018] Optionally, a seventh flow control valve is installed on the pipeline connecting the sodium hydroxide solution input device and the inlet of the coupled reactor to control the flow rate of the sodium hydroxide solution input to the coupled reactor.

[0019] Optionally, the coupled reactor is equipped with a pH transmitter.

[0020] Optionally, the jacket of the supergravity dynamic membrane reactor is provided with a first heat exchange liquid inlet and a first heat exchange liquid outlet.

[0021] The jacket of the dynamic tubular reactor is provided with a second heat exchange liquid inlet and a second heat exchange liquid outlet.

[0022] Optionally, the hypergravity dynamic membrane reactor is equipped with a first thermometer and a first pressure gauge;

[0023] The dynamic tubular reactor is equipped with a second thermometer and a second pressure gauge.

[0024] Optionally, the organic phase outlet of the first centrifugal separator is connected to the inlet of the dynamic tubular reactor, and the aqueous phase outlet of the first centrifugal separator is connected to a first water storage tank.

[0025] The organic phase outlet of the second centrifuge is connected to an organic phase storage tank, and the aqueous phase outlet of the second centrifuge is connected to a second water storage tank.

[0026] Secondly, embodiments of the present invention provide a physical field-enhanced waste oil pretreatment method, comprising pretreating the input waste oil using any of the physical field-enhanced waste oil pretreatment devices described above.

[0027] Optionally, the pretreatment of the input waste oil includes the following steps:

[0028] Waste oil is fed into a solid-liquid separator via a waste oil input device, allowing the organic phase separated by the solid-liquid separator to enter a high-gravity dynamic membrane reactor.

[0029] Demulsifier is introduced into the hypergravity dynamic membrane reactor through a demulsifier input device, purified water is introduced into the hypergravity dynamic membrane reactor through a purified water input device, and demetallizing agent is introduced into the hypergravity dynamic membrane reactor through a demetallizing agent input device.

[0030] Sodium hydroxide solution is introduced into the coupling reactor through a sodium hydroxide solution input device, so that the organic phase in the coupling reactor reacts under the coupling effect of sodium hydroxide solution and physical field;

[0031] Hydrogen peroxide is introduced into the dynamic tubular reactor through a hydrogen peroxide input device, and a demetallizing agent is introduced into the dynamic tubular reactor through a demetallizing agent input device, so that the organic phase separated by the first centrifuge enters the dynamic tubular reactor for further reaction.

[0032] The pretreated organic phase is obtained through a second centrifuge.

[0033] Optionally, the step of introducing the demetallizing agent into the hypergravity dynamic membrane reactor via the demetallizing agent input device includes:

[0034] A demetallizing agent containing phosphoric acid, citric acid, and oxalic acid is introduced into the hypergravity dynamic membrane reactor through a demetallizing agent input device.

[0035] Optionally, the demetallizing agent is a mixture of phosphoric acid at a concentration of 65% to 90%, citric acid at a concentration of 30% to 60%, and oxalic acid at a concentration of 40% to 60%.

[0036] Optional, also includes:

[0037] By controlling the opening of the seventh flow control valve, the pH value measured by the pH transmitter of the coupled reactor is made to be 5 to 6.

[0038] The beneficial effects of the above-described technical solutions provided in the embodiments of the present invention include at least the following:

[0039] (1) The waste oil pretreatment device with enhanced physical field provided in the embodiments of the present invention includes a physical field coupling unit. Through the coupling effect of physical field and demetallizing agent, the removal of metal ions is more thorough, which provides a guarantee for the smooth progress of subsequent hydrogenation reaction.

[0040] (2) The waste oil pretreatment device with enhanced physical field provided in this embodiment of the invention includes a waste oil input unit, a hypergravity dynamic membrane reactor unit, a physical field coupling unit, and a dynamic tubular reactor unit connected in sequence. Through the enhancement of physical field and the optimized design of the reactor unit, the removal rate of metal ions is improved, and continuous production of waste oil pretreatment is realized. Among them, the hypergravity dynamic membrane reactor has a high rotation speed, which can quickly and fully mix the materials, improve the reaction rate and reaction effect; the dynamic tubular reactor has a small reactor cavity width, and the micro-channels can realize efficient and rapid mass and heat transfer, making the reaction more thorough; therefore, the combination of the dynamic tubular reactor and the hypergravity dynamic membrane reactor realizes rapid heat exchange in the reaction process, improving the reaction rate and reaction effectiveness.

[0041] (3) Traditional processes require multiple washing and centrifugation operations, making the entire production process cumbersome, energy-intensive, and increasing the difficulty of equipment maintenance. The physical field-enhanced waste oil pretreatment device provided in this embodiment of the invention achieves continuous operation by introducing a hypergravity dynamic membrane reactor and a dynamic tubular reactor, greatly simplifying the process steps, realizing continuous feeding and discharging, and reducing the need for multiple washing and centrifugation operations. This not only reduces the complexity of the process but also reduces equipment wear and maintenance costs; at the same time, the reduction in the number of washing and centrifugation operations significantly reduces the amount of wastewater generated, reducing environmental pressure and wastewater treatment costs.

[0042] (4) The physical field-enhanced waste oil pretreatment method provided in this embodiment of the invention realizes continuous feeding and discharging, and can start or stop production as required, realizing continuous control of the production process, improving the level of production automation, avoiding unnecessary subsequent processing, and improving production efficiency.

[0043] Other features and advantages of the invention will be set forth in the description which follows, and will be apparent in part from the description, or may be learned by practicing the invention. The objects and other advantages of the invention may be realized and obtained by means of the structures particularly pointed out in the written description, claims, and drawings.

[0044] The technical solution of the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. Attached Figure Description

[0045] The accompanying drawings are provided to further illustrate the invention and form part of the specification. They are used in conjunction with embodiments of the invention to explain the invention and do not constitute a limitation thereof. In the drawings:

[0046] Figure 1 This is a schematic diagram of the physical field-enhanced waste oil pretreatment device in Embodiment 1 of the present invention;

[0047] Figure 2 This is a flowchart of the waste oil pretreatment method enhanced by physical field in Embodiment 2 of the present invention. Detailed Implementation

[0048] Exemplary embodiments of the present disclosure will now be described in more detail with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art.

[0049] It should be understood that the terminology used in this invention is merely for describing particular embodiments and is not intended to limit the invention. Furthermore, with respect to numerical ranges in this invention, it should be understood that each intermediate value between the upper and lower limits of the range is also specifically disclosed. Every smaller range between any stated value or intermediate value within a stated range, and any other stated value or intermediate value within said range, is also included in this invention. The upper and lower limits of these smaller ranges may be independently included or excluded from the range.

[0050] Unless otherwise stated, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. While only preferred methods and materials have been described herein, any methods and materials similar or equivalent to those described herein may be used in the implementation or testing of this invention. All references to this specification are incorporated by way of citation to disclose and describe methods and / or materials associated with those references. In the event of any conflict with any incorporated reference, the content of this specification shall prevail.

[0051] In the description of this invention, it should be noted that the terms "comprising", "including", "having", "containing", etc., are all open-ended terms, meaning that they include but are not limited to.

[0052] This invention provides a physical field-enhanced waste oil pretreatment device and method, which significantly improves the removal effect of impurities such as metal ions, has a simple process flow, low operation complexity, high production efficiency, low wastewater generation, and low energy consumption.

[0053] Example 1

[0054] Embodiment 1 of the present invention provides a waste oil pretreatment device enhanced by physical field, comprising a waste oil input unit, a hypergravity dynamic membrane reaction unit, a physical field coupling unit, and a dynamic tubular reaction unit connected in sequence, the specific structure of which is described in detail below. Figure 1 As shown.

[0055] (1) Waste oil input unit

[0056] It includes a waste oil input device 1 and a solid-liquid separator 3. A first flow control valve 2 is installed on the pipeline connecting the waste oil input device 1 and the inlet of the solid-liquid separator 3 to control the flow rate of waste oil input to the solid-liquid separator 3. The solid outlet of the solid-liquid separator 3 is connected to a solid collection device 4.

[0057] (2) Hypergravity dynamic membrane reaction unit

[0058] It includes a supergravity dynamic membrane reactor 11, and a demulsifier input device 5, a purified water input device 7, and a demetallizer input device 9, which are respectively connected to its inlet.

[0059] The organic phase outlet of the solid-liquid separator 3 is connected to the inlet of the supergravity dynamic membrane reactor 11.

[0060] A second flow control valve 6 is installed on the pipeline connecting the demulsifier input device 5 and the inlet of the hypergravity dynamic membrane reactor 11 to control the flow rate of the demulsifier input to the hypergravity dynamic membrane reactor 11.

[0061] A third flow control valve 8 is installed on the pipeline connecting the purified water input device 7 and the inlet of the hypergravity dynamic membrane reactor 11 to control the flow rate of purified water input to the hypergravity dynamic membrane reactor 11.

[0062] A fourth flow control valve 10 is installed on the pipeline connecting the demetallizer input device 9 and the inlet of the hypergravity dynamic membrane reactor 11 to control the flow rate of the demetallizer input to the hypergravity dynamic membrane reactor 11.

[0063] Furthermore, the jacket of the supergravity dynamic membrane reactor 11 is provided with a first heat exchange liquid inlet 12 and a first heat exchange liquid outlet 13, which are used to heat the fluid inside the reactor through the heat exchange liquid.

[0064] Waste oil or other heat exchange fluids can be used.

[0065] The supergravity dynamic membrane reactor 11 is equipped with a first thermometer 14 and a first pressure gauge 15.

[0066] (3) Physical field coupling unit

[0067] It includes a coupled reactor 18 to which an external physical field is applied and a sodium hydroxide solution input device 16 connected to its inlet.

[0068] Specifically, the physical field applied outside the coupling reactor 18 is an electric field.

[0069] Furthermore, the coupling reactor 18 is equipped with a pH transmitter 19, and a seventh flow control valve 17 is installed on the pipeline connecting the sodium hydroxide solution input device 16 and the inlet of the coupling reactor 18 to control the flow rate of the sodium hydroxide solution input to the inlet of the coupling reactor 18.

[0070] (4) Dynamic tubular reaction unit

[0071] It includes a dynamic tubular reactor 25 and a hydrogen peroxide inlet device 22 connected to its inlet.

[0072] The demetallizing agent input device 9 is also connected to the inlet of the dynamic tubular reactor 25.

[0073] A fifth flow control valve 24 is installed on the pipeline connecting the demetallizing agent input device 9 and the inlet of the dynamic tubular reactor 25 to control the flow rate of the demetallizing agent input to the dynamic tubular reactor 25; a sixth flow control valve 23 is installed on the pipeline connecting the hydrogen peroxide input device 22 and the inlet of the dynamic tubular reactor 25 to control the flow rate of the hydrogen peroxide input to the dynamic tubular reactor 25.

[0074] The jacket of the dynamic tubular reactor 25 is equipped with a second heat exchange liquid inlet 31 and a second heat exchange liquid outlet 32, which are used to heat the fluid inside the dynamic tubular reactor 25 through the heat exchange liquid. The heat exchange liquid can be waste oil or other heat exchange liquids.

[0075] The dynamic tubular reactor is equipped with a second thermometer 26 and a second pressure gauge 27.

[0076] A first centrifugal separator 20 is connected between the outlet of the coupled reactor 18 and the inlet of the dynamic tubular reactor 25, and a second centrifugal separator 28 is connected between the outlet of the dynamic tubular reactor 25.

[0077] Furthermore, the organic phase outlet of the first centrifugal separator 20 is connected to the inlet of the dynamic tubular reactor 25, and the aqueous phase outlet of the first centrifugal separator 20 is connected to the first water storage tank 21; the organic phase outlet of the second centrifugal separator 28 is connected to the organic phase storage tank 30, and the aqueous phase outlet of the second centrifugal separator 28 is connected to the second water storage tank 29.

[0078] The physical field enhanced waste oil pretreatment device provided in Embodiment 1 of the present invention includes a physical field coupling unit. Through the coupling effect of the physical field and the demetallizing agent, the removal of metal ions is more thorough, which provides a guarantee for the smooth progress of the subsequent hydrogenation reaction.

[0079] The physical field-enhanced waste oil pretreatment device provided in Embodiment 1 of this invention includes a waste oil input unit, a hypergravity dynamic membrane reactor unit, a physical field coupling unit, and a dynamic tubular reactor unit connected in sequence. Through the physical field enhancement effect and optimized design of the reactor units, the removal rate of metal ions is improved, while continuous production of waste oil pretreatment is achieved. The hypergravity dynamic membrane reactor has a high rotational speed, enabling rapid and thorough mixing and reaction of various materials, thus improving the reaction rate and effect. The dynamic tubular reactor has a small reactor cavity width, and the microchannels enable efficient and rapid mass and heat transfer, making the reaction more complete. Therefore, the combination of the dynamic tubular reactor and the hypergravity dynamic membrane reactor achieves rapid heat exchange during the reaction process, improving the reaction rate and the effectiveness of the reaction.

[0080] Traditional processes require multiple washing and centrifugation operations, making the entire production process cumbersome, energy-intensive, and increasing equipment maintenance difficulty. The physical field-enhanced waste oil pretreatment device provided in Embodiment 1 of this invention achieves continuous operation by introducing a hypergravity dynamic membrane reactor and a dynamic tubular reactor, significantly simplifying the process steps. It enables continuous feeding and discharging and reduces the need for multiple washing and centrifugation operations. This not only reduces process complexity but also reduces equipment wear and maintenance costs. Simultaneously, the reduction in the number of washing and centrifugation operations significantly reduces wastewater generation, thus reducing environmental impact and wastewater treatment costs.

[0081] Example 2

[0082] Embodiment 2 of the present invention provides a physical field-enhanced waste oil pretreatment method, comprising using any of the physical field-enhanced waste oil pretreatment devices described in Embodiment 1 to pretreat the input waste oil. For details, see... Figure 2 As shown, it includes the following steps:

[0083] Step S21: Input waste oil into the solid-liquid separator through the waste oil input device, so that the organic phase separated by the solid-liquid separator enters the ultragravity dynamic membrane reactor.

[0084] Waste oil enters the solid-liquid separator 3 from the waste oil input device 1 through the first flow control valve 2 at a flow rate of 50-100 g / min for filtration. The filtered solid impurities are discharged to the solid collection device 4 through the solid outlet, and the filtered organic phase flows into the ultragravity dynamic membrane reactor 11.

[0085] Step S22: Input demulsifier into the hypergravity dynamic membrane reactor through the demulsifier input device, input purified water into the hypergravity dynamic membrane reactor through the purified water input device, and input demetallizer into the hypergravity dynamic membrane reactor through the demetallizer input device.

[0086] Demulsifier is introduced into the hypergravity dynamic membrane reactor 11 through demulsifier input device 5 and second flow control valve 6 at a flow rate of 0.5-1 g / min; purified water is introduced into the hypergravity dynamic membrane reactor 11 through purified water input device 7 and third flow control valve 8 at a flow rate of 0.5-1 g / min; and demetallizing agent is introduced into the hypergravity dynamic membrane reactor 11 through demetallizing agent input device 9 and fourth flow control valve 10 at a flow rate of 0.8-5 g / min.

[0087] Furthermore, the demetallizing agent can be a mixture of phosphoric acid, citric acid, and oxalic acid. The concentration of phosphoric acid is 65%–90%, the concentration of citric acid is 30%–60%, and the concentration of oxalic acid is 40%–60%.

[0088] The material reacts fully in the hypergravity dynamic membrane reactor 11. The heat exchange liquid enters the jacket of the hypergravity dynamic membrane reactor 11 through the first heat exchange liquid inlet 12 and exchanges heat with the material entering the hypergravity dynamic membrane reactor 11. After heat exchange, the heat exchange liquid is discharged from the first heat exchange liquid outlet 13. The first temperature gauge 14 and the first pressure gauge 15 monitor the temperature and pressure in the hypergravity dynamic membrane reactor 11, respectively. The reaction products enter the coupling reactor 18.

[0089] Step S23: Sodium hydroxide solution is introduced into the coupling reactor through the sodium hydroxide solution input device, so that the organic phase in the coupling reactor reacts under the coupling effect of sodium hydroxide solution and physical field.

[0090] A physical field, specifically an electric field, is applied outside the coupling reactor 18. The removal of metal ions is enhanced by the physical field coupling using a demetallizing agent. Simultaneously, sodium hydroxide solution is introduced into the coupling reactor 18 via the sodium hydroxide solution inlet device 16 and the seventh flow control valve 17. A pH transmitter 19 transmits the pH value within the coupling reactor 18 to the seventh flow control valve 17. By controlling the opening of the seventh flow control valve 17, the pH value measured by the pH transmitter 19 in the coupling reactor 18 is kept between 5 and 6.

[0091] The product after reaction in the coupled reactor 18 enters the first centrifugal separator 20 for separation of the aqueous phase and the organic phase. The organic phase enters the dynamic tubular reactor 25, and the aqueous phase enters the first water storage tank 21.

[0092] Step S24: Hydrogen peroxide is introduced into the dynamic tubular reactor through the hydrogen peroxide input device, and demetallizing agent is introduced into the dynamic tubular reactor through the demetallizing agent input device, so that the organic phase separated by the first centrifuge enters the dynamic tubular reactor for further reaction.

[0093] Hydrogen peroxide is introduced into the dynamic tubular reactor 25 through the hydrogen peroxide input device 22 and the sixth flow control valve 23 at a flow rate of 0.2 to 0.8 g / min. Alternatively, 50% hydrogen peroxide can be introduced.

[0094] Simultaneously, through the demetallizing agent input device 9 and the fifth flow control valve 24, a demetallizing agent is input into the dynamic tubular reactor 25 at a flow rate of 2-5 g / min to enhance the removal of metal ions.

[0095] The material reacts fully in the dynamic tubular reactor 25. The heat exchange liquid enters the jacket of the dynamic tubular reactor 25 through the second heat exchange liquid inlet 31 and exchanges heat with the material entering the dynamic tubular reactor 25. After heat exchange, the heat exchange liquid is discharged from the second heat exchange liquid outlet 32. The second temperature gauge 26 and the second pressure gauge 27 monitor the temperature and pressure in the dynamic tubular reactor 25, respectively. The reaction product enters the second centrifugal separator 28.

[0096] Step S25: Obtain the pretreated organic phase through a second centrifuge.

[0097] The organic phase after centrifugation by the second centrifuge 28 is discharged into the organic phase storage tank 30, and the aqueous phase is discharged into the second water storage tank 29.

[0098] The physical field-enhanced waste oil pretreatment method provided in Embodiment 2 of the present invention enables continuous feeding and discharging, allows production to be started or stopped as required, achieves continuous and controllable production process, improves the level of production automation, avoids unnecessary subsequent processing, and improves production efficiency.

[0099] Application Example 1

[0100] 100 g / min of raw oil, 0.5 g / min of demulsifier, 0.5 g / min of purified water, and 1 g / min of demetallizing agent (a mixture of 85% phosphoric acid, 40% citric acid, and 50% oxalic acid) were introduced into a hypergravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85°C, and the residence time was 10 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 15 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 5 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the aforementioned demetallizing agent was introduced at 0.5 g / min, along with 50% hydrogen peroxide at 2 g / min. After a residence time of 10 minutes at 85°C, the reactor was centrifuged at 10,000 rpm for 5 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 95.69%.

[0101] Application Example 2

[0102] 50 g / min of raw oil, 0.5 g / min of demulsifier, 0.5 g / min of purified water, and 1 g / min of demetallizing agent (a mixture of 85% phosphoric acid, 40% citric acid, and 50% oxalic acid) were introduced into a hypergravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85°C, and the residence time was 20 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 30 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 10 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the aforementioned demetallizing agent was introduced at 0.5 g / min, along with 50% hydrogen peroxide at 2 g / min. After a residence time of 20 minutes at 85°C, the reactor was centrifuged at 10,000 rpm for 10 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 97.35%.

[0103] Application Example 3

[0104] 100 g / min of raw oil, 1 g / min of demulsifier, 1 g / min of purified water, and 2 g / min of demetallizing agent (a mixture of 85% phosphoric acid, 40% citric acid, and 50% oxalic acid) were introduced into a hypergravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85°C, and the residence time was 10 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 15 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 5 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the aforementioned demetallizing agent was introduced at 1 g / min, along with 50% hydrogen peroxide at 4 g / min. After a residence time of 10 minutes at 85°C, the reactor was centrifuged at 10,000 rpm for 5 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 96.72%.

[0105] Application Example 4

[0106] 100 g / min of raw oil, 1 g / min of demulsifier, 1 g / min of purified water, and 0.8 g / min of demetallizing agent (a mixture of 65% phosphoric acid, 30% citric acid, and 40% oxalic acid) were introduced into a hypergravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85°C, and the residence time was 10 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 15 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 5 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the above demetallizing agent was introduced at 2 g / min, and 50% hydrogen peroxide was introduced at 0.2 g / min. After a residence time of 10 minutes at 85°C, the reactor was centrifuged at 10,000 rpm for 5 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 95.69%.

[0107] Application Example 5

[0108] 100 g / min of raw oil, 1 g / min of demulsifier, 1 g / min of purified water, and 5 g / min of demetallizing agent (a mixture of 85% phosphoric acid, 50% citric acid, and 60% oxalic acid) were introduced into a hypergravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85°C, and the residence time was 10 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 10 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 5 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the above-mentioned demetallizing agent was introduced at 5 g / min, along with 0.8 g / min of 50% hydrogen peroxide. After a residence time of 15 minutes at 85°C, the reactor was centrifuged at 10,000 rpm for 5 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 95.9%.

[0109] Application Example 6

[0110] 100 g / min of raw oil, 1 g / min of demulsifier, 1 g / min of purified water, and 10 g / min of demetallizing agent (a mixture of 90% phosphoric acid, 60% citric acid, and 60% oxalic acid) were introduced into a high-gravity dynamic membrane reactor for mixing and reaction. The temperature was maintained at 85℃, and the residence time was 10 minutes. The product flowing out of the reactor outlet was then placed in a coupled reactor where the pH was adjusted to 5-6, and the residence time was 15 minutes. Under the enhancement of the physical field, further removal of metal ions was achieved. Subsequently, centrifugation was performed at 10,000 rpm for 5 minutes. After centrifugation, the product was introduced into a dynamic tubular reactor, and the above demetallizing agent was introduced at 8 g / min, and 50% hydrogen peroxide was introduced at 1 g / min. After a residence time of 10 minutes at 85℃, the reactor was centrifuged at 10,000 rpm for 5 minutes. The organic phase was collected for analysis, and the metal ion removal rate was 91.2%.

[0111] It should be understood that the specific order or hierarchy of steps in the disclosed process is an example of an exemplary method. Based on design preferences, it should be understood that the specific order or hierarchy of steps in the process may be rearranged without departing from the scope of this disclosure. The appended method claims provide elements of various steps in an exemplary order and are not intended to limit the scope to the specific order or hierarchy described.

[0112] In the detailed description above, various features are combined together in a single embodiment to simplify this disclosure. This approach to disclosure should not be construed as reflecting an intention that embodiments of the claimed subject matter require more features than are explicitly stated in each claim. Rather, as reflected in the appended claims, the invention is presented with fewer features than all of the features in a single disclosed embodiment. Therefore, the appended claims are hereby explicitly incorporated into the detailed description, with each claim representing a separate preferred embodiment of the invention.

[0113] The foregoing description includes examples of one or more embodiments. It is certainly impossible to describe all possible combinations of components or methods in order to describe the above embodiments, but those skilled in the art will recognize that further combinations and arrangements of the various embodiments are possible. Therefore, the embodiments described herein are intended to cover all such changes, modifications, and variations falling within the scope of the appended claims. Furthermore, the term “comprising” as used in the specification or claims is interpreted in a manner similar to the term “including,” as it is understood when used as a conjunction in the claims. Additionally, the use of any term “or” in the specification of the claims is intended to mean “non-exclusive or.” The terms “first,” “second,” etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

Claims

1. A waste oil pretreatment device enhanced by a physical field, characterized in that, It includes a waste oil input unit, a hypergravity dynamic membrane reaction unit, a physical field coupling unit, and a dynamic tubular reaction unit connected in sequence. The waste oil input unit includes a waste oil input device and a solid-liquid separator; The supergravity dynamic membrane reaction unit includes a supergravity dynamic membrane reactor and a demulsifier input device, a purified water input device, and a demetallizer input device respectively connected to its inlet. The organic phase outlet of the solid-liquid separator is connected to the inlet of the ultragravity dynamic membrane reactor; The physical field coupling unit includes a coupling reactor to which an external physical field is applied and a sodium hydroxide solution input device connected to its inlet; The dynamic tubular reaction unit includes a dynamic tubular reactor and a hydrogen peroxide input device connected to its inlet. The demetallizing agent input device is also connected to the inlet of the dynamic tubular reactor. A first centrifugal separator is connected between the outlet of the coupled reactor and the inlet of the dynamic tubular reactor. A second centrifugal separator is connected to the outlet of the dynamic tubular reactor.

2. The apparatus as claimed in claim 1, characterized in that, A first flow control valve is installed on the pipeline connecting the waste oil input device and the inlet of the solid-liquid separator. The solid outlet of the solid-liquid separator is connected to a solid collection device.

3. The apparatus as described in claim 2, characterized in that, A second flow control valve is installed on the pipeline connecting the demulsifier input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of the demulsifier input to the hypergravity dynamic membrane reactor. A third flow control valve is installed on the pipeline connecting the purified water input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of purified water input to the hypergravity dynamic membrane reactor. A fourth flow control valve is installed on the pipeline connecting the demetallizing agent input device and the inlet of the hypergravity dynamic membrane reactor to control the flow rate of the demetallizing agent input to the hypergravity dynamic membrane reactor. A fifth flow control valve is installed on the pipeline connecting the demetallizing agent input device and the inlet of the dynamic tubular reactor to control the flow rate of the demetallizing agent input to the dynamic tubular reactor; A sixth flow control valve is installed on the pipeline connecting the hydrogen peroxide input device and the inlet of the dynamic tubular reactor to control the flow rate of hydrogen peroxide input to the dynamic tubular reactor.

4. The apparatus as described in claim 3, characterized in that, A seventh flow control valve is installed on the pipeline connecting the sodium hydroxide solution input device and the inlet of the coupled reactor to control the flow rate of the sodium hydroxide solution input to the coupled reactor.

5. The apparatus as described in claim 4, characterized in that, The coupled reactor is equipped with a pH transmitter.

6. The apparatus as claimed in claim 1, characterized in that, The jacket of the supergravity dynamic membrane reactor is provided with a first heat exchange liquid inlet and a first heat exchange liquid outlet. The jacket of the dynamic tubular reactor is provided with a second heat exchange liquid inlet and a second heat exchange liquid outlet.

7. The apparatus as claimed in claim 6, characterized in that, The hypergravity dynamic membrane reactor is equipped with a first thermometer and a first pressure gauge. The dynamic tubular reactor is equipped with a second thermometer and a second pressure gauge.

8. The apparatus as claimed in claim 1, characterized in that, The organic phase outlet of the first centrifugal separator is connected to the inlet of the dynamic tubular reactor, and the aqueous phase outlet of the first centrifugal separator is connected to a first water storage tank. The organic phase outlet of the second centrifuge is connected to an organic phase storage tank, and the aqueous phase outlet of the second centrifuge is connected to a second water storage tank.

9. A method for pretreating waste oil using a physically enhanced field, characterized in that, The invention includes a waste oil pretreatment device that utilizes the physical field enhancement described in any one of claims 1 to 8 to pretreat the input waste oil.

10. The method as described in claim 9, characterized in that, The pretreatment of the input waste oil includes the following steps: Waste oil is fed into a solid-liquid separator via a waste oil input device, allowing the organic phase separated by the solid-liquid separator to enter a high-gravity dynamic membrane reactor. Demulsifier is introduced into the hypergravity dynamic membrane reactor through a demulsifier input device, purified water is introduced into the hypergravity dynamic membrane reactor through a purified water input device, and demetallizing agent is introduced into the hypergravity dynamic membrane reactor through a demetallizing agent input device. Sodium hydroxide solution is introduced into the coupling reactor through a sodium hydroxide solution input device, so that the organic phase in the coupling reactor reacts under the coupling effect of sodium hydroxide solution and physical field; Hydrogen peroxide is introduced into the dynamic tubular reactor through a hydrogen peroxide input device, and a demetallizing agent is introduced into the dynamic tubular reactor through a demetallizing agent input device, so that the organic phase separated by the first centrifuge enters the dynamic tubular reactor for further reaction. The pretreated organic phase is obtained through a second centrifuge.

11. The method as described in claim 10, characterized in that, The process of introducing a demetallizing agent into the hypergravity dynamic membrane reactor via a demetallizing agent input device includes: A demetallizing agent containing phosphoric acid, citric acid, and oxalic acid is introduced into the hypergravity dynamic membrane reactor through a demetallizing agent input device.

12. The method as described in claim 11, characterized in that, The demetallizing agent is a mixture of phosphoric acid at a concentration of 65%–90%, citric acid at a concentration of 30%–60%, and oxalic acid at a concentration of 40%–60%.

13. The method as described in claim 10, characterized in that, Also includes: By controlling the opening of the seventh flow control valve, the pH value measured by the pH transmitter of the coupled reactor is made to be 5 to 6.

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