CN119799362A - A purification method and integrated purification system for white oil decolorization and membrane separation to remove oil mist - Google Patents
A purification method and integrated purification system for white oil decolorization and membrane separation to remove oil mist Download PDFInfo
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Abstract
The invention discloses a purification method and an integrated purification system for white oil decolorization and membrane separation to remove oil mist. The method comprises the steps of heating recovered oil by a preheater, mixing clay and the recovered oil by a pre-mixing kettle, taking a part of the pre-mixed liquid as reflux liquid, stirring and heating the pre-mixed liquid by a decoloring kettle to form decoloring liquid and decoloring tail gas, separating the decoloring liquid by a filter cake layer filter to form clay waste residue, white oil and filter cake tail gas, separating the filter cake tail gas and the decoloring tail gas by a pre-separator to form white oil and separated gas, condensing the separated gas by a condenser to form white oil and noncondensable gas, separating the noncondensable gas by a membrane separation device to form white oil and discharged oil gas, filtering clay particles in the white oil by a white oil filter, and recycling the white oil. The purification method and the integrated purification system provided by the invention can be used for carrying out decolorization treatment on the recovered oil obtained after the methylene dichloride is rectified, and recovering the white oil component from the tail gas generated in the decolorization process to obtain the white oil.
Description
Technical Field
The invention relates to a purification method for decoloring white oil and separating and removing oil mist by a membrane, and also relates to an integrated purification system for realizing the purification method, belonging to the technical field of extraction and recovery.
Background
The white oil decoloring device is auxiliary equipment matched with a wet lithium battery diaphragm production line and an extraction liquid recovery device. In the production process of the lithium battery diaphragm, white oil is used as a pore-forming agent, methylene dichloride is used as an extracting agent, and the generated extracting solution contains methylene dichloride, white oil, a small amount of water, polyethylene impurities and the like.
In the Chinese invention with the patent number ZL 202210833314.4, a continuous white oil decoloring system and a continuous white oil decoloring method are disclosed. The technical scheme includes that a decoloring tower and a continuous filtering discharging device connected with the decoloring tower are arranged, an oil inlet and a compressed air inlet are arranged at the upstream of the continuous filtering discharging device, and a hydrocyclone, a clear oil outlet and a dirty oil outlet are connected at the downstream of the continuous filtering discharging device. The method comprises the steps of filling oil into a first filtering tank, circularly obtaining clear oil, filtering, switching to a second filtering tank, drying a filter cake of the first filtering tank by compressed air, decompressing and discharging slag for standby, and circularly carrying out corresponding operations from switching to the second filtering tank. The system adopts two filter tanks for coupling design, and changes the original intermittent treatment process into a continuous process, and oil inlet and oil outlet are continuously carried out.
In addition, in the chinese invention of patent No. ZL 201910681806.4, a clay mixing device for grease decolorization is disclosed. The device includes the agitator tank, and one side of agitator tank is equipped with the jar of premixing, and the top of premixing jar is equipped with the carclazyte metering cylinder, and carclazyte metering cylinder's top and bottom communicate with carclazyte jar and jar of premixing respectively. The communication part of the clay metering cylinder and the premixing tank is provided with a conical diffusion plate. The bottom of the premixing tank is provided with a conical hopper. One side of the premixing tank is provided with an oil injection pipe which is communicated with the premixing tank in a horizontal inscribed manner. The oil filling pipe and the clay metering cylinder are arranged diagonally. The premixing tank, the stirring tank, the conical diffusion plate and the blades are all provided with anti-adhesion coatings. The clay is mixed and stirred in the premixing tank in a diffusion mode, the pressure of oil is utilized to be injected into the premixing tank in a horizontal inscription mode, and the stirring effect is improved by utilizing vortex.
However, in the production process of white oil products, the conventional white oil decoloring device and oil mist removing equipment still have the problems of low decoloring efficiency and incomplete oil mist removal, which seriously affect the production efficiency and the product quality.
Disclosure of Invention
The primary technical problem to be solved by the invention is to provide a purification method for decoloring white oil and removing oil mist through membrane separation.
Another technical problem to be solved by the present invention is to provide an integrated purification system for implementing the above purification method.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
According to a first aspect of an embodiment of the present invention, there is provided a method for purifying white oil decolorization and membrane separation to remove oil mist, comprising the steps of:
S1, receiving the recovered oil from a main line by using a raw material tank, and heating the recovered oil by using a preheater;
S2, mixing clay and reclaimed oil by using a premixing kettle to form premixing tail gas and premixing liquid, and inputting a part of premixing liquid serving as reflux liquid into the premixing kettle;
step S3, stirring and heating the premixed liquid and the premixed tail gas by using a decoloring kettle to decolor the white oil component to form decoloring liquid and decoloring tail gas;
S4, separating the decolorized solution by using a filter cake layer filter to form clay waste residue, white oil and filter cake tail gas;
S5, separating filter cake tail gas and decolored tail gas by using a preseparator to form white oil and separated gas;
s6, condensing the separated gas by using a condenser to form white oil and noncondensable gas;
S7, separating noncondensable gas by using membrane separation equipment to form white oil and discharged oil gas;
s8, filtering out clay particles in the white oil by using a white oil filter, and recycling the white oil;
The fluid in the preseparator spirally descends in a mode of forming a spiral direction included angle alpha with the horizontal plane, and the fluid in the condenser spirally descends in a mode of forming a spiral direction included angle beta with the horizontal plane, and the condition that alpha is smaller than beta is met, so that the flow rates of the fluid and the condenser are close.
Wherein preferably, when the filter cake tail gas and the decolorized tail gas are input into the preseparator, a venturi tube is utilized to increase the flow rate.
According to a second aspect of the embodiment of the invention, an integrated purification system for white oil decolorization and membrane separation to remove oil mist is provided, which comprises a raw material tank, a preheater, a premixing kettle, a decolorization kettle, a filter cake layer filter, a white oil filter, a preseparator, a condenser and membrane separation equipment, wherein,
The feed inlet of the raw material tank is connected with an upstream process pipeline, and the discharge outlet of the raw material tank is connected with the feed inlet of the preheater; the first discharge port is connected with the first feed port of the decoloring kettle and the reflux port of the premixing kettle, and the second discharge port is connected with the second feed port of the decoloring kettle;
The first discharge port of the filter cake layer filter is connected with a downstream process pipeline, the second discharge port of the filter cake layer filter is connected with the feed port of the white oil filter, and the third discharge port of the filter cake layer filter is connected with the feed port of the preseparator;
The first discharge port of the preseparator is connected with the feed port of the white oil filter, the second discharge port of the preseparator is connected with the feed port of the condenser, the first discharge port of the condenser is connected with the feed port of the white oil filter, the second discharge port of the condenser is connected with the feed port of the membrane separation equipment, the first discharge port of the membrane separation equipment is connected with the feed port of the white oil filter, the second discharge port of the membrane separation equipment is connected with a downstream oil-gas discharge pipeline, and the discharge port of the white oil filter is connected with a downstream white oil recovery tank;
The pre-separator comprises a separator and a guide plate, wherein the guide plate is arranged on the inner wall of the separator and is spiral from top to bottom, and an included angle alpha is formed between the guide plate and the rotation direction of the horizontal plane;
The condenser comprises a cylinder body, a condensing pipe and a baffle plate, wherein the condensing pipe is arranged in the cylinder body along the vertical direction, the baffle plate is arranged on the inner wall of the cylinder body, is spiral from top to bottom, and has a beta included angle with the rotation direction of a horizontal plane, so that alpha < beta is satisfied to form a similar flow velocity.
Preferably, the rotation direction included angle alpha=30°, and the rotation direction included angle beta=42°.
Wherein preferably, the preseparator further comprises a venturi, wherein,
The venturi tube comprises an inlet, a contraction section, a throat, a diffusion section and an outlet, wherein the inlet is connected with a feed inlet of the preseparator, the outlet is connected with a feed inlet of the preseparator, the diameter of the inlet is D, the diameter of the throat is D1, the diameter of the outlet is D2, the included angle of a conical tube of the contraction section is A1, the included angle of a conical tube of the diffusion section is A2, and D > D2> D1 and A1> A2.
Wherein preferably the origin of the deflector or one of the segments is disposed directly below the outlet of the venturi.
Wherein preferably the outlet of the venturi is located at the top of the preseparator and is arranged such that fluid exiting the venturi flows directly along the helical path of the baffle as it enters the separator.
Wherein preferably, the membrane separation device comprises a vacuum unit and a plurality of membrane separation units, wherein,
A plurality of the membrane separation units are connected in parallel, and the vacuum unit is connected in series with the membrane separation units;
The air inlet of the membrane separation unit is connected with the feed inlet of the membrane separation device, the air outlet is connected with the second discharge outlet of the membrane separation device, the concentrated gas outlet of the central tube is connected with the air inlet of the vacuum unit, and the air outlet of the vacuum unit is connected with the first discharge outlet of the membrane separation device.
Wherein preferably the membrane separation unit comprises a plurality of lipophilic separation membranes, wherein,
The separation membranes are bent into a plurality of layers of concentric circles, the separation membranes are concentrically and alternately arranged in the membrane separation units to form air channels and white oil channels, the air channels are communicated with the air inlets and the air outlets of the membrane separation units, and the white oil channels are communicated with the concentrated gas outlets of the central pipes of the membrane separation units.
Compared with the prior art, the method has the technical effects that firstly, the recovered white oil is purified to the reusable standard through the decoloring treatment, the recycling of resources is effectively realized, the purchasing cost of raw materials of enterprises is reduced, the economic benefit is improved, secondly, the white oil component in the tail gas can be efficiently recovered by adopting the multi-stage treatment processes of pre-separation, condensation, membrane separation and the like aiming at the tail gas generated in the decoloring process, the resource utilization rate is further improved, the emission gas is ensured to reach the standard, the environmental pollution is reduced, thirdly, the special structural design of the pre-separator and the condenser, such as a spiral guide plate and a specific spiral included angle, and the application of a venturi tube in the pre-separator, remarkably enhances the oil-gas separation effect, improves the processing efficiency and the stability of the whole system, and fourthly, the use of a multi-layer lipophilic separation membrane in the membrane separation device can efficiently separate the white oil under the condition of low oil content, further solves the problems of low decoloring efficiency, incomplete cleaning and the like existing in the conventional white oil device and the degreasing fog mist removal device, and the like, and is particularly suitable for cleaning the fine white oil mist production and has high requirements on the fine chemical industry.
Drawings
FIG. 1 is a schematic diagram of an integrated purification system for white oil decolorization and membrane separation to remove oil mist according to a first embodiment of the present invention;
FIG. 2 is a schematic diagram of the membrane separation unit of FIG. 1;
FIG. 3 is a schematic view of the membrane separation unit of FIG. 2 in cross section perpendicular to the longitudinal direction;
FIG. 4 is a schematic diagram of a preseparator according to a second embodiment of the present invention;
FIG. 5 is a schematic view of the venturi of FIG. 4;
fig. 6 is a schematic structural view of a condenser according to a second embodiment of the present invention.
Detailed Description
The technical contents of the present invention will be described in detail with reference to the accompanying drawings and specific examples.
The technical concept of the invention is that aiming at dichloromethane white oil extract (containing dichloromethane, white oil, a small amount of water, polyethylene impurities and the like) generated by a wet lithium battery diaphragm production line, after the recovery by dichloromethane rectification, the obtained recovery oil is subjected to decolorization and oil mist removal treatment so as to recover the white oil therein and enable the white oil to reach the reusable standard. Specifically, the recovered oil is refined by comprehensively utilizing a decoloring kettle, a filter, a demister and membrane separation equipment. And simultaneously, aiming at tail gas containing white oil mist generated in the decoloring process, recovering the white oil component in the tail gas through a multistage treatment process so as to realize the efficient utilization of resources and the up-to-standard emission. Particularly, the invention focuses on recycling the white oil in the tail gas containing the white oil mist, and even if the white oil content in the tail gas is lower than 500mg/m < 3 >, the problem of low recycling efficiency of conventional equipment can be overcome by an innovative treatment mode, so that the economic and efficient white oil recycling is realized.
First embodiment
As shown in fig. 1, the integrated purification system for white oil decolorization and membrane separation to remove oil mist provided in the first embodiment of the present invention includes a raw material tank 1, a preheater 2, a pre-mixing tank 3, a decolorization tank 4, a cake layer filter 5, a white oil filter 6, a pre-separator 7, a condenser 8 and a membrane separation device 9.
The feed inlet 11 of the feed tank 1 is connected to an upstream process line for receiving the main recovery oil upstream. The discharge port 12 is connected with a feed port 21 of the preheater 2.
The preheater 2 is a heating device and comprises a material pipeline and a medium pipeline. Wherein, both ends of the material pipeline are a feed inlet 21 and a discharge outlet 22 of the preheater 2. The medium lines connect the medium lines upstream and downstream of the preheater 2 for passage of a heat exchange medium, such as steam or heat transfer oil. The feed inlet 21 of the preheater 2 is connected with the discharge outlet 12 of the raw material tank 1, and the discharge outlet 22 is connected with the first feed inlet 31 of the premixing kettle 3.
The premixing kettle 3 is a mixing device for chemical raw materials and comprises a kettle body, a homogenizer, a gear motor, a temperature sensor and a plurality of feeding and discharging ports. Wherein, the first feed inlet 31 of the premixing kettle 3 is connected with the material outlet 22 of the preheater 2, the second feed inlet 32 is connected with an upstream process pipeline, the first discharge outlet 33 is connected with the first feed inlet 41 of the decoloring kettle 4 and the reflux outlet 35 of the premixing kettle 3, and the second discharge outlet 34 is connected with the second feed inlet 42 of the decoloring kettle 4.
The decoloring kettle 4 is a decoloring device for chemical raw materials and comprises a kettle body, a homogenizer, a gear motor, a temperature sensor, a medium pipeline and a plurality of feeding and discharging ports. Wherein, the first feed inlet 41 of decoloration cauldron 4 connects the first discharge gate 33 of premix cauldron 3, and the second feed inlet 42 connects the second discharge gate 34 of premix cauldron 3, and the feed inlet 51 of filter cake layer filter 5 and the backward flow mouth 45 of decoloration cauldron 4 are connected to first discharge gate 43, and the feed inlet 71 of preseparation 7 is connected to second discharge gate 44. The medium line of the decolorizing kettle 4 connects the medium lines upstream and downstream of the decolorizing kettle 4 to pass a heat exchange medium, such as steam or heat transfer oil.
The filter cake layer filter 5 is a solid-liquid separation device. The feed inlet 51 of the filter cake layer filter 5 is connected with the first discharge port 43 of the decoloring kettle 4, the first discharge port 52 is connected with a downstream process pipeline, the second discharge port 53 is connected with the feed inlet 61 of the white oil filter 6, and the third discharge port 54 is connected with the feed inlet 71 of the preseparator 7.
The preseparator 7 is a gas-liquid separation device, such as a cyclone, for agglomerating droplets in the gas, so that the droplets are separated from the gas. The feed inlet 71 of the preseparator 7 is connected with the third discharge outlet 54 of the filter cake layer filter 5, the first discharge outlet 72 is connected with the feed inlet 61 of the white oil filter 6, and the second discharge outlet 73 is connected with the feed inlet 81 of the condenser 8.
The condenser 8 is a gas condensing device and comprises a medium pipeline and a material pipeline. Wherein the medium line connects the medium line upstream and downstream of the condenser 8 for passing a heat exchange medium, such as cold water. The feed inlet 81 (material pipeline) of the condenser 8 is connected with the second discharge outlet 73 of the preseparator 7, the first discharge outlet 82 (material pipeline) is connected with the feed inlet 61 of the white oil filter 6, and the second discharge outlet 83 (material pipeline) is connected with the feed inlet 91 of the membrane separation device 9.
The membrane separation device 9 is a semi-permeable membrane gas separation device, and includes a vacuum unit 94 and a plurality of membrane separation units 95. The feed inlet 91 of the membrane separation device 9 is connected with the second discharge outlet 83 of the condenser 8, the first discharge outlet 92 is connected with the feed inlet 61 of the white oil filter 6, and the second discharge outlet 93 is connected with a downstream oil gas discharge pipeline. The membrane separation units 95 are connected in parallel, the vacuum unit 94 is connected in series with the membrane separation units 95, and the vacuum unit 94 provides a negative pressure environment for the membrane separation units 95 so that white oil components in the noncondensable gas permeate the separation membranes and are enriched to form white oil.
As shown in fig. 2 and 3, in the membrane separation device 9 provided by the embodiment of the present invention, the air inlet 951 of the membrane separation unit 95 is connected to the feed inlet 91 of the membrane separation device 9, the air outlet 952 is connected to the second discharge outlet 93 of the membrane separation device 9, the central tube concentrated air outlet 953 is connected to the air inlet of the vacuum unit 94, and the air outlet of the vacuum unit 94 is connected to the first discharge outlet 92 of the membrane separation device 9.
The membrane separation unit 95 includes a plurality of lipophilic separation membranes 954 capable of separating organic and inorganic components in a gas. The multi-layered separation membrane 954 is bent into multi-layered concentric circles, and concentrically and alternately arranged in the membrane separation unit 95 to form an air passage 954a and a white oil passage 954b. Wherein the air channel 954a is in communication with the air inlet 951 and the air outlet 952, and the white oil channel 954b is in communication with the center tube enriched air outlet 953.
The white oil filter 6 is a solid-liquid separation device for removing clay particles in the white oil. The feed inlet 61 of the white oil filter 6 is connected with the second discharge outlet 53 of the filter cake layer filter 5, the first discharge outlet 72 of the preseparator 7, the first discharge outlet 82 of the condenser 8 and the first discharge outlet 92 of the membrane separation device 9, and the discharge outlet 62 is connected with the downstream white oil recovery tank.
The raw material tank 1 receives the recovered oil from the upstream through the feed inlet 11, and is input into a material pipeline of the preheater 2 through the discharge outlet 12 and the feed inlet 21 of the preheater 2, and is output as a preheated mixture through the discharge outlet 22 of the preheater 2. The heating medium in the medium pipeline of the preheater 2 exchanges heat with the recovered oil in the material pipeline to heat the recovered oil into a preheated mixed liquid. The main component of the recovered oil comprises white oil with decolorization.
The pre-mixing kettle 3 is fed with the pre-heating mixed liquid through a first feed inlet 31, is fed with clay through a second feed inlet 32, and is mixed by a homogenizer to separate pre-mixing tail gas and pre-mixing liquid. The main components of the premixed tail gas comprise air and white oil mist, and the main components of the premixed liquid comprise white oil to be decolorized and carclazyte. The premixed tail gas is input into the decoloring kettle 4 through a second discharge port 34 of the premixing kettle 3 and a second feed port 42 of the decoloring kettle 4. The premix liquid is output from the first discharge port 33 of the premix kettle 3, one part of the premix liquid is input into the decolorizing kettle 4 from the first feed port 41 of the decolorizing kettle 4, and the other part of the premix liquid is input into the premix kettle 3 from the return port 35 of the premix kettle 3, so that the premix efficiency is improved.
The premixed liquid and the premixed tail gas which are input into the decoloring kettle 4 are mixed and stirred by a homogenizer to decolor the white oil component, and the decolored tail gas and the decolored liquid are separated. Wherein, the main components of the decolorized tail gas comprise air and white oil mist, and the main components of the decolorized liquid comprise decolorized white oil and clay waste residue. The decolorized tail gas is input into the preseparator 7 through the second discharge port 44 of the decolorization kettle 4 and the feed port 71 of the preseparator 7. The decolorization liquid is output from the first discharge port 43 of the decolorization kettle 4, one part of the decolorization liquid is input into the filter cake layer filter 5 from the feed port 51 of the filter cake layer filter 5, and the other part is input into the decolorization kettle 4 from the reflux port 45 of the decolorization kettle 4, so that the decolorization efficiency is improved. The heating medium in the medium pipeline of the decoloring kettle 4 exchanges heat with the decoloring material to maintain the decoloring material in the decoloring kettle 4 at a design temperature and improve the decoloring efficiency.
The decolorized solution fed into the cake layer filter 5 is separated into clay waste residue (cake), white oil and cake tail gas. The main components of the filter cake tail gas comprise air and white oil mist. The clay waste residue is conveyed to a downstream pipeline through a first discharge hole 52, white oil is input into the white oil filter 6 through a second discharge hole 53 and a feed hole 61 of the white oil filter 6, and filter cake tail gas is input into the preseparator 7 through a third discharge hole 54 and a feed hole 71 of the preseparator 7.
The filter cake tail gas and the decolored tail gas which are input into the preseparator 7 are subjected to condensation and separation of white oil mist liquid drops therein under the action of the preseparator 7, so that white oil and separation gas are formed. Wherein the main components of the separated gas comprise air and white oil mist. The white oil is fed into the white oil filter 6 through the first discharge port 72 and the feed port 61 of the white oil filter 6, and the separated gas is fed into the condenser 8 through the second discharge port 73 and the feed port 81 of the condenser 8.
The medium pipeline and the material pipeline of the condenser 8 are subjected to sufficient heat exchange to condense the separation gas in the material pipeline, so that white oil and noncondensable gas are formed. Wherein the main components of the noncondensable gas comprise air and white oil mist. The white oil is fed into the white oil filter 6 through the first discharge port 82 and the feed port 61 of the white oil filter 6, and the separated gas is fed into the membrane separation device 9 through the second discharge port 83 and the feed port 91 of the membrane separation device 9.
The vacuum unit 94 of the membrane separation device 9 provides a negative pressure environment for the membrane separation unit 95, that is, the pressure of the white oil channel 954b is lower than that of the air channel 954a, the non-condensable gas is input from the feed inlet 91 of the membrane separation device 9 (the air inlet 951 of the membrane separation unit 95), and is separated and enriched by the separation membrane 954, and separated into white oil and discharged oil gas. The white oil is discharged from the center tube concentrate outlet 953 by the negative pressure of the vacuum unit 94, and is introduced into the white oil filter 6 through the vacuum unit 94. The discharged oil gas is discharged through the air outlet 952 and the second discharge port 93.
Because the oil content in the oil mist is greatly reduced after the oil is removed by multiple separation, the environment with lower oil content is more favorable for the separation membrane 954 to exert the advantage of selective permeation, thereby further improving the oil removal rate. In addition, the oil mist is accelerated by the upstream equipment and matched with the pressure regulating device at the inlet of the membrane separation equipment 9, so that the oil mist reaches the pressure and the wind speed which are most suitable for separation by the separation membrane 954.
The white oil filter 6 filters and removes clay particles possibly existing in the white oil, and the white oil is output to the white oil recovery tank through the discharge port 62.
Second embodiment
This embodiment is different from the above embodiment in that the structures of the preseparator 7 and the condenser 8 provided in the embodiment of the present invention are further optimized to improve recovery efficiency.
As shown in fig. 4 and 5, the preseparator 7 includes a venturi 710, a separator 720, and a baffle 730. Wherein separator 720 is the separation device of preseparator 7. The baffle 730 is disposed on the inner wall of the separator 720, and has a spiral shape from top to bottom, and an included angle α with the horizontal plane. The venturi 710 is a feed device to the preseparator 7, the outlet of which is located at the top of the preseparator 7 and is arranged such that the fluid exiting the venturi 710 is able to flow directly along the spiral path of the baffle 730 when entering the separator 720. In other words, the beginning of the baffle 730 or one of the segments should be installed just below the outlet of the venturi 710 to ensure a smooth transition of the fluid directly into the spiral channel, reducing the local resistance to take advantage of the hydrodynamic effect created by the venturi 710. Also, the installation angles and positions of the deflector 730 and the venturi 710 need to be precisely adjusted to optimize the fluid flow path.
The venturi 710 includes an inlet 711, a constriction 712, a throat 713, a diffuser 714, and an outlet 715, which, due to their physical characteristics, are capable of increasing the flow rate of fluid therethrough. Wherein inlet 711 is connected to feed 71 of preseparator 7 and outlet 715 is connected to feed of separator 720. The diameter of the inlet 711 is D, the diameter of the throat 713 is D1, the diameter of the outlet 715 is D2, the angle of the tapered tube of the constriction 712 is A1, and the angle of the tapered tube of the diffusion 714 is A2. D > D2> D1, A1> A2. According to Bernoulli's principle, an increase in flow velocity results in a decrease in pressure, thereby creating a low pressure zone in the converging portion (converging section 712) of the venturi. In the low pressure zone, liquid dissolved or entrained in the gas is more prone to droplet formation.
A venturi 710 is provided at the inlet 71 of the preseparator 7 to effect separation of oil droplets by its velocity increasing and outlet adsorption. Since the white oil droplets have a larger specific gravity than air, the velocity increase with respect to air is slower in the velocity increase stage through the throat 713, so that they can be separated from air, and thus a single separation is achieved. When passing through the outlet 715, the white oil droplets which are also heavier are adsorbed less, so that the white oil droplets are easier to sink and separate under the action of gravity, and secondary separation is realized. Preferably, in order that the separated oil drops flow on the pipe wall more easily and are discharged cumulatively, the oil drops do not stay on the pipe wall due to the viscosity of the white oil, and the air flow speed is affected, so that an oil-proof smooth coating is added on the pipe wall and the deflector 730.
Preferably, d2=0.65d, d1=0.3d, a1=24°, a2=10.5°. According to experimental analysis, when the design parameters of the venturi 710 meet the above parameters, the oil-gas separation efficiency of the preseparator 7 is highest and the energy loss is smallest.
Notably, the venturi 710 is utilized to significantly accelerate the fluid and, at high flow speeds, by abruptly changing the direction of flow, droplets (vaporized white oil) in the fluid will continue to move in the original direction due to inertia and separate from the gas (because the gas readily changes direction of flow). The preseparator 7 uses the characteristics to condense and separate the white oil mist droplets in the filter cake tail gas and the decolored tail gas (tail gas mixed into white oil mist containing tail gas), and adsorb the white oil mist droplets onto the deflector 730 to form white oil and separated gas. And the structural characteristics of the venturi 710 allow the cake off-gas and decolorized off-gas flow rates entering the preseparator 7 to be increased, thus enhancing separation efficiency.
In particular, the mass of the oil droplets is much larger than the gas molecules, so that the inertia of the oil droplets is larger when the gas flow is accelerated, and it is difficult to change the motion state rapidly with the gas flow. The gas molecules can respond to the change of the flow speed rapidly due to small mass and move along with the gas flow. As the air flow passes through the venturi throat 713, the air flow velocity increases sharply, while the velocity of the oil droplets increases more slowly due to the greater inertia. This velocity differential causes a relative motion between the oil droplets and the gas, with the oil droplets gradually "lagging" from the gas stream and being separated.
The oil droplets are subjected to mainly inertial, drag and gravitational forces in the air stream. During the throat 713 acceleration phase, the drag increases rapidly, but the change in motion state lags behind the gas due to the large inertia of the oil droplets. When the airflow velocity is high enough, the drag experienced by the oil droplets is insufficient to overcome the inertia, resulting in the "pull-out" of the oil droplets from the airflow. The separated oil drops are settled under the action of gravity or are adsorbed by the wall surface of the venturi 710 and the deflector 730, so as to realize separation.
The spiral baffle 730, which extends the path of the fluid entering the preseparator 7, increases the residence time of the fluid in the preseparator 7, which provides more time for the droplets to settle, and the droplets have more opportunities to settle in the spiral path, reducing the likelihood of being re-entrained by the gas, thereby improving separation efficiency. The baffle 730 promotes collision and aggregation between droplets by enhancing the vortex effect in the preseparator 7, thereby improving the settling efficiency of droplets so that droplets are more likely to settle to the bottom of the preseparator 7.
As shown in fig. 6, the condenser 8 includes a cylinder 810, a condensing duct 820, and a baffle 830. The condensing pipe 820 is connected to a medium pipe and disposed in the cylinder 810 in a vertical direction, so that the heat exchange medium in the condensing pipe 820 cools the separated gas in the cylinder 810. Baffle 830 is disposed on the inner wall of barrel 810, and is spiral from top to bottom, and has an included angle β with the horizontal plane.
The separated gas separated by the pre-separator 7 is condensed by the condensing pipe 820 and is in a spiral descending form in the condenser 8 by the baffle plate 830, and the oil-gas separation effect is further enhanced by using centrifugal force.
Preferably, α < β. The baffle 730 and the baffle 830 are both spiral devices, and because of the obstruction of the condenser pipe 820, the rotation direction included angle of the baffle 830 needs to be larger than that of the baffle 730, so that similar flow velocity is formed, and a higher gas-liquid separation effect is achieved.
More preferably, α=30°, β=42°. According to experimental verification, the gas and oil drop separation effect is best when the angle of rotation direction is alpha=30°, and beta=42°.
Third embodiment
A third embodiment of the present invention provides a purification method for decoloring white oil and removing oil mist by membrane separation, which at least comprises the following steps.
Step S1, receiving the recovered oil from the main line by using a raw material tank 1, and heating the recovered oil by using a preheater 2;
S2, mixing clay and reclaimed oil by using a premixing kettle 3 to form premixing tail gas and premixing liquid, and inputting a part of premixing liquid serving as reflux liquid into the premixing kettle 3;
Step S3, stirring and heating the premixed liquid and the premixed tail gas by using a decoloring kettle 4 to decolor the white oil component to form decoloring liquid and decoloring tail gas;
s4, separating the decolorized solution by using a filter cake layer filter 5 to form clay waste residue, white oil and filter cake tail gas;
s5, separating the filter cake tail gas and the decolored tail gas by using a preseparator 7 to form white oil and separated gas;
The angle alpha between the direction of rotation of the fluid in the preseparator 7 and the horizontal plane is the angle alpha, and the spiral descends.
S6, condensing the separated gas by using a condenser 8 to form white oil and noncondensable gas;
The angle beta between the fluid in the condenser 8 and the horizontal plane is the spiral direction, and the spiral descends. Preferably, α < β. More preferably, α=30°, β=42°.
S7, separating non-condensable gas by using membrane separation equipment 9 to form white oil and discharged oil gas;
And S8, filtering out clay particles in the white oil by using a white oil filter 6, and recycling the white oil.
In summary, according to the purification method and the integrated purification system for decoloring white oil and separating and removing oil mist by using a membrane provided by the embodiment of the invention, the reclaimed white oil is decolored to reach the reuse standard, so that the effective recycling and utilization of resources are realized, and the raw material purchasing cost of enterprises is reduced. And (3) separating, condensing and separating the tail gas formed in the decoloring process by a membrane, so that the white oil in the tail gas is further recovered, and the economic benefit is improved.
It should be noted that the above embodiments are only examples. The technical schemes of the embodiments can be combined, and all the technical schemes are within the protection scope of the invention.
The term "forming" used herein means that the material can be obtained by one of various processes, and is not limited to the processes shown in the examples. The sequence of the steps of the present invention may be changed according to actual needs, the sequence of the steps may be changed, and serial processing may be changed to parallel processing, which is not limited to the sequence of the steps listed in the embodiments.
The terms "upper," "lower," "horizontal," "vertical," "top," "bottom," and the like refer to an orientation or positional relationship based on that shown in the drawings, for convenience of description and simplicity of description, and do not necessarily indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus should not be construed as limiting the invention.
Furthermore, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
The purification method and the integrated purification system for decoloring white oil and separating and removing oil mist by a membrane are described in detail. Any obvious modifications to the present invention, without departing from the spirit thereof, would constitute an infringement of the patent rights of the invention and would take on corresponding legal liabilities.
Claims (9)
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