CN212236086U - Unsteady-state feeding part emulsified liquid-liquid two-phase separation system - Google Patents
Unsteady-state feeding part emulsified liquid-liquid two-phase separation system Download PDFInfo
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- CN212236086U CN212236086U CN202020837154.7U CN202020837154U CN212236086U CN 212236086 U CN212236086 U CN 212236086U CN 202020837154 U CN202020837154 U CN 202020837154U CN 212236086 U CN212236086 U CN 212236086U
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Abstract
The utility model relates to a liquid-liquid two-phase separation system for partial emulsification of unsteady feeding, which comprises a pre-separation tank, a collection tank, an extrusion emulsion breaking device, a centrifuge and a recovery tank, wherein the centrifuge is also communicated with the circulation tank which is communicated with the pre-separation tank; the pre-separation tank is communicated with a separation liquid inlet pipe, and the separation liquid inlet pipe and the circulating tank respectively extend into the bottom of the pre-separation tank through corresponding insertion pipes; a first baffle and a second baffle are arranged in the pre-separation tank, the first baffle is close to the position of the insertion pipe, and the second baffle is close to one side of the heavy component aggregation package; the pre-separation tank is communicated with the heavy component collecting tank through a siphon pipe. The utility model can greatly improve the production efficiency, improve the separation thoroughness and reduce the size of the equipment; meanwhile, the stability of system operation and the feeding adaptability are greatly improved, and the working condition with large fluctuation range can be met.
Description
Technical Field
The utility model belongs to the technical field of chemical production, specific saying so relates to a liquid-liquid double-phase piece-rate system of emulsification of unsteady state feeding part.
Background
The separation of two-phase and multi-phase liquid-phase mixtures is a necessary processing skill in modern chemical production processes. For liquid phase mixture needing high separation, modern chemical engineering mostly adopts a rectification mode for separation and purification, and the remarkable characteristics are high precision of separated products, high energy consumption and large one-time investment related to a self-control system. For the application field with low requirement on separation precision, especially for the separation of a mixing system with low self-compatibility of a liquid phase, more density difference under the action of a gravity field can be applied for standing separation; the method has the obvious characteristics of low energy consumption, large occupied area and incapability of achieving very effective separation under the condition of partial emulsification. The application of the high-speed centrifugal machine in the field of industrial separation perfectly solves the problem of limited field by replacing the original action of a gravity field through centrifugal force, and greatly improves the production efficiency.
In the existing liquid-liquid separation process, an industrial centrifuge forms an operation principle of a fuzzy physical separation interface by acting strong centrifugal force in a machine, so that the requirement on the working condition of a feeding state is high when the industrial centrifuge operates, the change of the flow and components at a feeding end can cause the damage of the formed effective separation interface, the separation purity of one side after centrifugal separation is rapidly changed, and possible material pollution or environmental pollution accidents such as material running and the like are caused. The field use of the centrifugal machine under variable working conditions is limited. Simultaneously centrifuge self can't thoroughly separate the material under the emulsification state that has formed, to the high operating mode of material own emulsification sensitivity even, centrifuge normal operating condition in very short time with material tangential zero velocity reach with centrifuge rotational speed equal process, have very big tangential shearing force, aggravate the emulsification process of material, make originally the separable material of gravity field appear local emulsification and can't separate, further restricted industrial centrifuge's application.
The applicant has encountered remarkably the problems of the above-described process in the process of treating the very low concentration polymer solution-sewage-dispersant mixture produced by the apparatus during the production of the hydrogenated styrene-conjugated diene block copolymer. Because of the presence of small amounts of polymer, no purification treatment can be used; natural sedimentation requires a large field and sedimentation time, and has no industrial application value; direct centrifugal treatment, the aggravation of emulsification and extreme instability of the feeding state cause that a centrifugal machine system can not normally operate completely. The production of the complete set of devices is severely hampered by the problem of separation.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects of the prior art, the utility model provides a liquid-liquid two-phase separation system which can demulsify the emulsifier and realize the emulsification of the unsteady feeding part of automatic pre-separation and centrifugal unilateral/bilateral control.
The utility model utilizes the separation principle that two liquid phase components are not completely mutually soluble and can be mostly kept stand for layering, and introduces a high-efficiency centrifugal separation device and a forced demulsification device through design to achieve the purpose of high-efficiency separation, thereby greatly improving the production efficiency, improving the separation thoroughness and reducing the equipment size; simultaneously the utility model discloses an ingenious design only needs to improve centrifuge one side export separation degree and guarantees the separation precision, need not consider the operation conditions who taboos other one side, makes the stability of system operation, feeding adaptability increase substantially, can satisfy the undulant operating mode of great scope.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a liquid-liquid two-phase separation system for partial emulsification of unstable feeding comprises a pre-separation tank, a collection tank, an extrusion demulsification device, a centrifugal machine and a recovery tank, wherein the centrifugal machine is communicated with the circulation tank which is communicated with the pre-separation tank; the pre-separation tank is communicated with a separation liquid inlet pipe, the separation liquid inlet pipe and the circulating tank respectively extend into the bottom of the pre-separation tank through corresponding insertion pipes, static electricity caused by direct entering from the top of the pre-separation tank is eliminated, and liquid level fluctuation is avoided; a first baffle and a second baffle are arranged in the pre-separation tank, the first baffle is close to the position of the insertion pipe, and the second baffle is close to one side of the heavy component aggregation package; the pre-separation tank is communicated with the heavy component collecting tank through a siphon.
The utility model discloses during the use: the mixture to be separated firstly enters a pre-separation tank for preliminary sedimentation and pre-separation, and the free components are kept stand and separated into phases; a baffle structure is designed in the pre-separation tank, one side of the baffle is provided with components with higher density, and the density difference is calculated by using a Bernoulli equation to design the siphon height through density calculation; the high-density components separated by siphoning can enter a deep centrifugal or rectifying device if deep separation is required; the light component crosses over the upper edge of the baffle under the action of buoyancy to form a light component phase, and then the light component phase is further subjected to deep separation treatment; the components after pre-separation form two phases respectively, and the components are basically stable when entering the subsequent deep separation; after passing through the extrusion demulsification device, part of emulsified components are divided into two phases through resin fillers under the action of front and back pressure difference and enter a centrifugal machine for deep separation; the specific gravity design of the centrifuge is that the light phase is recovered from the collected middle phase according to the requirements of working conditions, the other side enters the pre-separation tank again to participate in the pre-separation, the separation is circulated in the system, and finally the separation is carried out in the subsequent process from the concentrated pre-separation discharge port; when the separation of two phases has higher requirements, deep separation liquid is taken by a designed three-phase centrifuge, the other side of the three-phase centrifuge enters a pre-separation tank again for redistribution and separation, the separation is completely circulated in the system, and finally, recovery liquid obtained by deep separation is discharged out of the system. The small amount of solid or pasty impurities possibly existing in the system are separated by the slag discharge of the centrifuge, so that the purity of the system is higher in the accumulation process of the running time.
Preferably, the first baffle comprises an upper plate and a lower plate, the upper plate is of a non-porous plate structure, the lower plate is of a porous plate structure, and the porous plate can play a role in slowing flow.
Preferably, the second baffle is of a non-porous plate structure and can be used for isolating and separating light and heavy components.
Preferably, the upper plate and the lower plate are connected by bolts. The cleaning of the later-stage kettle feeding operation and the height control of the baffle are facilitated.
Preferably, the collecting tank comprises a light component collecting tank and a heavy component collecting tank, and the light component collecting tank and the heavy component collecting tank are provided with or without stirring devices; the pre-separation tank is respectively communicated with a light component collecting tank and a heavy component collecting tank, the light component collecting tank or the heavy component collecting tank is communicated with an extrusion demulsification device, the extrusion demulsification device is communicated with a centrifugal machine, and the centrifugal machine is communicated with a recovery tank; the heavy component collecting tank or the light component collecting tank is communicated with the circulating tank; the light component collecting tank or the heavy component collecting tank and the recovery tank are respectively communicated with a system recovery device; the centrifugal machine is communicated with the centrifugal machine slag tank.
Preferably, the collecting tank comprises a light component collecting tank and a heavy component collecting tank, and stirrers are arranged in the light component collecting tank and the heavy component collecting tank; the pre-separation tank is respectively communicated with a light component collecting tank and a heavy component collecting tank, the light component collecting tank is communicated with a first extrusion demulsification device, the first extrusion demulsification device is communicated with a first centrifugal machine, and the first centrifugal machine is communicated with a first recovery tank; the heavy component collecting tank is communicated with a second extrusion demulsification device, the second extrusion demulsification device is communicated with a second centrifugal machine, and the second centrifugal machine is communicated with a second recovery tank; the first centrifugal machine and the second centrifugal machine are respectively communicated with the circulating tank; the light component collecting tank, the first recovery tank, the heavy component collecting tank and the second recovery tank are respectively communicated with a system recovery device; the centrifugal machine is communicated with the centrifugal machine slag tank.
Preferably, the insertion pipes of the circulation tank and the insertion pipes of the separation liquid inlet pipe are arranged in parallel in the longitudinal direction. The distance between the baffles is ensured to ensure the standing time of the separation liquid.
Preferably, a specific gravity ring is arranged in the centrifuge, and the inner diameter of the specific gravity ring is controlled to be 90-110 mm. Through the specially designed specific gravity ring, the centrifuge inclines towards the target separation side during fuzzy physical interface interception, so that the separation precision is guaranteed, and the problem of separation precision and the problem of environmental pollution caused by material running on the other side can be avoided even if the three-phase centrifuge is changed in operation condition under the design.
Preferably, the pre-separation tank is of a horizontal tank structure, the collection tank is of a vertical tank structure, and the centrifuge is a three-phase centrifuge.
Preferably, the top of the light component collecting tank with stirring and the top of the heavy component collecting tank with stirring are reserved with corresponding tank bottom inlet pipe orifices. The feeding of the demulsifier is convenient.
The utility model discloses do special design to preseparation jar inner structure, the separation liquid and centrifuge export to preseparation jar adopt the mouth of pipe to compare other mouths of pipe for parallel, guarantee the distance between the baffle as far as possible and guarantee the stationary time of separation liquid, the separation liquid directly gets into preseparation jar bottom through the insert tube, eliminate the static that directly gets into from the tank top that crouches and arouse, avoid causing the liquid level to fluctuate simultaneously; the utility model discloses two baffles of design in the preseparation jar, first baffle are close to the insert tube position, and another baffle is close to heavy ends package one side of assembling, mainly is used for keeping apart the light and heavy components of separation. The top of the designed vertical tank with the stirring function is provided with a tank bottom inlet pipe orifice for the purpose of being used for a demulsifier feeding system; based on the principle of an atmospheric leg, the zero-pressure design of the communication between the demulsifier feeding and pre-preparing process and the atmosphere can be realized through the pressure balance calculation and automatic control setting of the system, and the safety and the operation convenience are greatly improved; the designed physical force-passing extrusion demulsification device has the characteristic of easy replacement of the filler, and can select the proper filler to perform demulsification according to different liquid phases.
Compared with the prior art, the beneficial effects of the utility model reside in that:
(1) the utility model has no requirement on the proportion of the feeding components, combines emulsion breaking and separation, has the characteristics of high degree of automatic control and strong operation stability, simultaneously has smaller occupied area, low equipment one-time investment cost and obvious operation economic benefit, and can realize the recovery except the treated materials with the recovery value;
(2) the centrifugal machine can separate high-purity light components or heavy components according to the needs, the components which are not completely separated through the system design enter the pre-separation tank again to participate in the pre-separation after circulating demulsification, and the components are completely separated;
(3) the utility model discloses can reduce centrifuge operation requirement by a wide margin under the prerequisite of fully guaranteeing the separation precision, can simplify centrifuge's design completely, reduce equipment cost by a wide margin, improve the operational reliability, only require one side export according to system design qualified can, opposite side export material accessible device carries out circulation treatment.
Drawings
FIG. 1 is a schematic structural view of a preseparation tank of the present invention;
FIG. 2 is a schematic diagram of the system structure of the present invention having a higher separation requirement for the light fraction side under the condition of unstable feeding component and feeding amount;
FIG. 3 is a schematic diagram of the system structure of the present invention having a higher separation requirement for one side of the heavy component under the condition of unstable feeding amount and feeding component;
FIG. 4 is a schematic diagram of the system structure of the present invention, which has higher separation requirements for light and heavy components under the condition of unstable feeding components and feeding amount;
fig. 5 is a schematic structural view of a specific gravity ring of the centrifuge.
Detailed Description
The present invention will be further described with reference to the following specific examples, but the scope of the present invention is not limited thereto. Those skilled in the art can and should understand that any simple changes or substitutions based on the spirit of the present invention should fall within the protection scope of the present invention.
Pre-separation horizontal tank design calculation
The size of the pre-separation horizontal tank equipment is calculated according to the required retention time and the maximum feeding amount, and the effective volume of the baffle side is ensured to be larger than the product of the retention time and the maximum feeding amount; the siphon port calculation is based on Bernoulli equation static pressure calculation principle, and the pre-separation horizontal tank structure is shown in figure 1.
Designing the siphon height to be H, the second baffle of the pre-separation tank to be H, and the position of the two-component interface layer to be at the percentage position x of the height of the second baffle; light density is rhoLight and lightweightHaving a heavy fraction density of rhoHeavy weight,Relative density ρ' ═ ρLight/unρHeavy load. Normal siphon work design height equation: then ρHeavy loadgh＝ρHeavy loadgxH+ρLight and lightweightg (1-x) H, wherein x is more than 0 and less than 1, and rho' is more than 0 and less than 1; after conversion, the siphon height H ═ H (x + ρ '- ρ' x) H can be calculated.
For example, in the case of cyclohexane-water separation, where the separation interface is controlled at 50% of the baffle, the siphon height can be calculated to be 0.89 times the height of the second baffle. Compare in the fixed siphon mouth of current technology, the utility model discloses it is different according to retrieving light and heavy component, the accessible is nimble to be adjusted the siphon mouth height and is guaranteed that light and heavy looks stew the layering time in the separating medium in the jar crouches to make the layering more thorough, for example when needing to retrieve light component, then need the upper strata light component to need longer time to stew, so can suitably reduce siphon mouth height.
Example 1
Deep separation of light components under variable working conditions
Referring to fig. 1, 2 and 5, the unsteady-state feeding part emulsified liquid-liquid two-phase separation system comprises a pre-separation tank 1, a light component collection tank 2, a heavy component collection tank 3, an extrusion demulsification device 4, a centrifuge 5 and a recovery tank 6, wherein the pre-separation tank 1 is of a horizontal tank structure, the light component collection tank 2 and the heavy component collection tank 3 are of a vertical tank structure, and the centrifuge is a three-phase centrifuge. The three-phase centrifuge 5 is communicated with a circulating tank 7, and the circulating tank 7 is communicated with the pre-separation tank 1; the pre-separation tank 1 is communicated with a separation liquid inlet pipe 8, the separation liquid inlet pipe 8 and the circulating tank 7 respectively extend into the bottom of the pre-separation tank through corresponding insertion pipes and directly enter the bottom of the pre-separation horizontal tank through the insertion pipes, static electricity caused by direct entering from the top of the pre-separation horizontal tank is eliminated, and liquid level fluctuation is avoided; the inserting pipes corresponding to the circulating tank 7 and the inserting pipes corresponding to the separating liquid inlet pipe 8 are arranged in parallel along the longitudinal direction, and the distance between the baffles is ensured to ensure the standing time of the separating liquid.
A first baffle 9 and a second baffle 10 are arranged in the pre-separation tank 1, the first baffle 9 is close to the position of the insertion pipe, and the second baffle 10 is close to one side of the heavy component aggregation package; the height of the second baffle plate 10 is higher than that of the first baffle plate 9, the first baffle plate 9 comprises an upper plate and a lower plate, the upper plate is of a non-porous plate structure, the lower plate is of a porous plate structure, and the porous plate can play a role in slowing flow; the upper plate and the lower plate are connected by bolts, so that the cleaning of the later kettle entering operation and the control of the height of the baffle are facilitated; the second baffle 10 is of a non-porous plate structure and can be used for isolating and separating light and heavy components. The preseparation tank is in communication with the heavy fraction collection tank 3 via a siphon 13.
The pre-separation tank 1 is respectively communicated with a light component collecting tank 2 and a heavy component collecting tank 3, the light component collecting tank 2 is provided with a stirring device, the heavy component collecting tank 3 is not provided with the stirring device, and a tank bottom inlet pipe orifice is reserved at the top of the light component collecting tank 2 with stirring and used for feeding a demulsifier; the light component collecting tank 2 is communicated with an extrusion demulsification device 4, the extrusion demulsification device 4 is communicated with a three-phase centrifuge 5, and the three-phase centrifuge 5 is communicated with a recovery tank 6; the heavy component collecting tank 3 is communicated with a circulating tank 7; the light component collecting tank 2 and the recovery tank 6 are respectively communicated with a system recovery device; the three-phase centrifuge 5 is communicated with a centrifuge slag tank 11.
A specific gravity ring 12 is arranged in the three-phase centrifuge, and the inner diameter of the specific gravity ring is controlled to be 90-110 mm according to the treatment capacity of the device and the requirement on light phase; through the specially designed specific gravity ring, the centrifuge inclines towards the target separation side during fuzzy physical interface interception, so that the separation precision is guaranteed, and the problem of separation precision and the problem of environmental pollution caused by material running on the other side can be avoided even if the three-phase centrifuge is changed in operation condition under the design.
In the embodiment, cyclohexane, water and a dispersing agent system are selected for separation, wherein the cyclohexane and the water are partially emulsified, the proportion of cyclohexane components fluctuates within the range of 20-80%, the middle value assumes 50%, the relative density is 0.78, the total feeding amount is 0.5-5 t/h, the middle value assumes 3t/h, the water is partially emulsified under the action of the dispersing agent and enters the cyclohexane light component, and the tested emulsified intermediate state relative density of the cyclohexane and the water is 0.79-0.85; the aim is to realize that the cyclohexane can be recycled after deep separation and the sewage can reach the standard and be discharged; this example extends cyclohexane to the light fraction described in the patent description and water to the heavy fraction described in the patent description.
The system starts to operate, water is injected into the pre-separation tank 1 from the circulating tank 7 or the separation liquid inlet pipe 8 (to-be-separated liquid inlet), and when the liquid level of the pre-separation tank 1 rises to exceed the height of the siphon inlet, the heavy component collecting tank 3 is formed by siphon to meet water to complete the preparation process. Then the materials to be separated are fed into the pre-separation tank 1 from the separation liquid inlet pipe 8 according to the normal treatment process to complete the pre-separation process of the materials to be separated.
Design preseparation tank stock capacity 15m3To ensure adequate pre-separation time. The light component that accomplishes preseparation strides over on the baffle along getting into light component collecting vessel 2, get into heavy component collecting vessel 3 behind the heavy component siphon, calculate according to the siphon, make the heavy component that must assemble completely just can get into heavy component collecting vessel 3, the water that heavy component collecting vessel 3 was collected is through the pump sending to external sewage treatment, water content maximum value when designing the pump delivery capacity and reaching the biggest feeding, namely pump delivery capacity 4t/h, the 3 liquid level automatic control of after-design pump frequency conversion and heavy component collecting vessel are correlated, can handle the complicated changeable state of feeding operating mode completely and lead to the variable of heavy component collecting vessel 3 separation water. The partially emulsified intermediate state can cross over the upper edge of a baffle plate to enter a light component collecting tank 2 in the time accumulation process, the light component collecting tank 2 forms relatively stable components under stirring, the components are fed into a three-phase centrifuge 5 after being forcedly physically extruded and demulsified through a pump set, the feed pump is designed to carry out appropriate amplification according to intermediate values, and the feed pump enters the three-phase centrifuge 5 for separation according to the feed amount of 2-3 t/h in the embodiment; when the centrifugal machine is automatically controlled, materials below the lower control light component collecting tank 2 start to enter a self-circulation state according to the lower liquid level protection design, the centrifugal machine is in a wet standby state at the moment, and the centrifugal machine enters normal work again when the liquid level of the light component collecting tank 2 is restored to the set control restoration liquid level, so that the purpose is to maximally protect the stability of the feeding amount of the centrifugal machine, and ensure the normal operation of the equipmentThe operation and the light phase end are stable. Meanwhile, the system can also ensure that the centrifuge fluctuates within a 20 percent +/-deviation feeding range through the buffer capacity of the liquid level of the light component collecting tank 2 during design and operation, and the light phase back pressure is increased when the light component material is taken until the light phase still reaches the required separation purity value when the upper limit value and the lower limit value of the fluctuation range.
And collecting a small amount of solid waste after three-phase centrifugation to a fixed container for periodic treatment. Collecting heavy components and residual small amount of emulsion breaking emulsion difficult to squeeze into circulation tank 7, adding demulsifier (such as CaCl) under stirring according to material properties2The solution enters the pre-separation tank 1 again to participate in pre-separation after further chemical demulsification is finished. And complete cyclohexane deep separation and recovery are sequentially completed in a circulating manner, and simultaneously the discharged sewage meets the discharge requirement.
Example 2
Operating method for implementing heavy grouping depth separation with variable working conditions
Referring to fig. 1, 3 and 5, another structure of an unsteady-state feeding partially emulsified liquid-liquid two-phase separation system is as shown in example 1, wherein the pre-separation tank 1 is respectively communicated with a light component collection tank 2 and a heavy component collection tank 3, the light component collection tank 2 is not provided with a stirring device, and the heavy component collection tank 3 is provided with a stirring device; the heavy component collecting tank 3 is communicated with an extrusion demulsification device 4, the extrusion demulsification device 4 is communicated with a three-phase centrifuge 5, and the three-phase centrifuge 5 is communicated with a recovery tank 6; the light component collecting tank 2 is communicated with a circulating tank 7; the light and heavy component collecting tank 3 and the recovery tank 6 are respectively communicated with a system recovery device; the three-phase centrifuge 5 is communicated with a centrifuge slag tank 11. A tank bottom inlet pipe orifice is reserved at the top of the heavy component collecting tank 3 with stirring and is used for feeding the demulsifier.
In this embodiment, cyclohexane, water and a compatibilizer system are selected for separation, wherein cyclohexane partially enters a water phase under the effect of the compatibilizer, so that sewage cannot reach an efflux condition; the proportion of water components in the fed sewage fluctuates within the range of 20-80%, the middle value assumes 50%, the total feeding amount is 0.5-5 t/h, the middle value assumes 3t/h, cyclohexane enters the sewage components under the action of a compatibilizer, and the tested solubilization intermediate state relative density of the cyclohexane and water is 0.88-0.95; the aim is to realize the standard discharge of COD in sewage and the recycling of cyclohexane; this example extends cyclohexane to the light fraction described in the patent description and water to the heavy fraction described in the patent description, the process flow being shown in figure 3.
The system starts to operate, water is injected into the pre-separation tank 1 from the circulating tank 7 or the separation liquid inlet pipe 8 (to-be-separated liquid inlet), siphoning is formed when the liquid level of the pre-separation tank 1 rises to exceed the height of the siphon inlet, and the heavy component collection tank 3 is subjected to water breakthrough to complete the preparation process. Then the materials to be separated are fed into the pre-separation tank 1 from the inlet of the liquid to be separated according to the normal treatment process, and the pre-separation process of the materials to be separated is completed.
Design pre-separation horizontal tank storage capacity of 30-45 m3To ensure adequate pre-separation time. The light component cyclohexane which is subjected to pre-separation is subjected to concentration and enrichment and then crosses the upper edge of the baffle plate to enter a light component collecting tank 2, and the water of the heavy component and the intermediate transition state of the cyclohexane and the water enter a heavy component collecting tank 3 after being siphoned. The cyclohexane collected by the light component collecting tank 2 is conveyed to a device system by a pump for recycling, the maximum cyclohexane content is designed when the pump conveying capacity reaches the maximum feeding capacity, namely the pump conveying capacity is 4t/h, the pump frequency conversion is designed to be associated with the liquid level automatic control of the tank B, and the variable of the light component collecting tank 2 for separating the cyclohexane caused by the complex and changeable state of the feeding working condition can be completely processed. Under the condition of time accumulation of the partially compatibilized intermediate state, the thickness increase of the intermediate state enters the heavy component collecting tank 3 through a siphon pipeline under the action of static pressure, and the heavy component collecting tank 3 forms a relatively stable component under stirring. Feeding the materials into a three-phase centrifuge 5 after forced phase splitting through physical extrusion by a pump set, wherein the feeding pump is designed to amplify the materials appropriately according to a middle value, and the materials are fed into the three-phase centrifuge 5 for separation according to 2-3 t/h of feeding amount calculated in the embodiment; according to the lower liquid level protection design during automatic control, the materials below the lower-control heavy component collecting tank 3 start to enter a self-circulation state, the centrifuge is in a wet standby state at the moment, and the heavy component collecting tank 3 enters normal work again when the liquid level is restored to the set control restoration liquid level, so that the purpose is to protect the stability of the feeding amount of the centrifuge 5 to the maximum extent, and the normal operation of equipment and the stability of a heavy phase end can be ensured. Meanwhile, the system can be designed and operatedThe buffer capacity of the liquid level of the heavy component collecting tank 3 ensures that the centrifuge is in a 20 percent +/-deviation feeding range fluctuation, and the heavy phase back pressure is increased when the heavy component material is taken until the heavy phase still reaches the separation purity requirement value when the heavy phase is in the upper limit value and the lower limit value of the fluctuation range.
And collecting a small amount of solid waste after three-phase centrifugation to a fixed container for periodic treatment. Light component cyclohexane and a small amount of residual intermediate state difficult to separate are collected into a circulating tank 7, a demulsifier is added according to the material property under stirring, and the solution enters a pre-separation tank 1 again to participate in pre-separation after further phase separation. Complete sewage discharge reaching the standard is completed according to the circulation, and cyclohexane recovery is realized.
Example 3
Light and heavy component deep separation implementation operation with variable working conditions
Referring to fig. 1, 4 and 5, another structure of a non-steady-state feeding partially-emulsified liquid-liquid two-phase separation system refers to example 1, wherein the collection tank comprises a light component collection tank 2 and a heavy component collection tank 3, and stirrers are arranged in the light component collection tank 2 and the heavy component collection tank 3; the pre-separation tank 1 is respectively communicated with a light component collecting tank 2 and a heavy component collecting tank 3, the light component collecting tank 2 is communicated with a first extrusion demulsification device 4-1, the first extrusion demulsification device 4-1 is communicated with a first centrifugal machine 5-1, and the first centrifugal machine 5-1 is communicated with a first recovery tank 6-1; the heavy component collecting tank 3 is communicated with a second extrusion demulsification device 4-2, the second extrusion demulsification device 4-2 is communicated with a second centrifugal machine 5-2, and the second centrifugal machine 5-2 is communicated with a second recovery tank 6-2; the first centrifugal machine 5-1 and the second centrifugal machine 5-2 are respectively communicated with a circulating tank 7; the light component collecting tank 2, the first recovery tank 6-1, the heavy component collecting tank 3 and the second recovery tank 6-2 are respectively communicated with a system recovery device; the first centrifugal machine 5-1 and the second centrifugal machine 5-2 are communicated with the corresponding centrifugal machine slag tanks. Tank bottom inlet pipe orifices are reserved at the tops of the light component collecting tank 2 with stirring and the heavy component collecting tank 3 with stirring respectively and used for feeding the demulsifier.
In this embodiment, cyclohexane, water, a compatibilizer, and a dispersant are selected to be separated in a coexisting system, wherein water can be partially emulsified into cyclohexane, and cyclohexane partially enters a water phase under the effect of the compatibilizer, so that wastewater cannot reach an efflux condition. The proportion of water components in the feed sewage fluctuates within the range of 20-80%, the middle value assumes 50%, the total feed amount is 0.5-5 t/h, and the middle value assumes 3 t/h; water is partially emulsified into a cyclohexane light component under the action of a dispersing agent, and the relative density of the tested emulsified intermediate state of cyclohexane and water is 0.79-0.85; under the action of the compatibilizer, enabling cyclohexane to enter sewage components, wherein the tested solubilizing intermediate state relative density of the cyclohexane and water is 0.88-0.95; there is no significant transition between the two intermediate states. The aim is to realize the deep separation of cyclohexane, recycle and discharge the sewage COD up to the standard; this example extends cyclohexane to the light fraction described in the patent description and water to the heavy fraction described in the patent description, the process flow being shown in figure 4.
The system starts to operate, water is injected into the pre-separation tank 1 from the circulating tank 7 or the separation liquid inlet pipe 8 (to-be-separated liquid inlet), siphoning is formed when the liquid level of the pre-separation tank 1 rises to exceed the height of the siphon inlet, and the heavy component collection tank 3 is subjected to water breakthrough to complete the preparation process. Then the materials to be separated are fed into the pre-separation tank from the inlet of the liquid to be separated according to the normal treatment process, and the pre-separation process of the materials to be separated is completed.
Design the storage capacity of the pre-separation tank to be 50-100 m3To ensure adequate pre-separation time. The light component cyclohexane which is pre-separated and the part of emulsified cyclohexane-water transition state with the density close to the cyclohexane cross the upper edge of the baffle to enter the light component collecting tank 2; the heavy component water and the cyclohexane with the density close to the water are increased to a water transition state, and enter a heavy component collecting tank 3 after siphoning. The light component collecting tank 2 forms relatively stable components under stirring, the components are subjected to forced physical extrusion demulsification through a pump set and then fed into a three-phase centrifuge 5-1, the feeding pump is designed to perform appropriate amplification according to intermediate values, and the light component collecting tank enters the three-phase centrifuge for separation according to the feeding amount of 2-3 t/h calculated in the embodiment; the heavy component collecting tank 3 forms relatively stable components under stirring, the components are subjected to physical phase splitting through forced extrusion by a pump set and then fed into a three-phase centrifuge 5-2, the feeding pump is designed to amplify a proper amount according to a middle value, and the heavy component enters the three-phase centrifuge for separation according to the feeding amount of 2-3 t/h calculated in the embodiment.When the centrifugal machine is automatically controlled, materials below the lower-control light component collecting tank 2/heavy component collecting tank 3 start to enter a self-circulation state according to a lower liquid level protection design, the centrifugal machine is in a wet standby state at the moment, and when the liquid level of the light component collecting tank 2/heavy component collecting tank 3 is recovered to a set control recovery liquid level, the centrifugal machine enters normal work again. Meanwhile, when the system is designed and operated, the centrifuge can be in a 20 percent +/-deviation feeding range fluctuation through the buffer capacity of the liquid levels of the light component collecting tank 2/the heavy component collecting tank 3, and the light phase and the heavy phase are regulated to reach the separation purity requirement value when the light phase and the heavy phase are respectively taken and reach the upper limit value and the lower limit value of the fluctuation range.
And collecting a small amount of solid waste after three-phase centrifugation to a fixed container for periodic treatment. Collecting light and heavy components and residual small amount of emulsion breaking emulsion difficult to squeeze into circulation tank 7, adding demulsifier (such as CaCl) under stirring according to material properties2The solution enters the pre-separation tank again to participate in pre-separation after further chemical demulsification and phase separation processes are finished. And complete cyclohexane deep separation and recovery are sequentially completed in a circulating manner, and simultaneously the discharged sewage meets the discharge requirement.
Claims (10)
1. An unsteady feed partially emulsified liquid-liquid two-phase separation system, characterized in that: the system comprises a pre-separation tank, a collection tank, an extrusion demulsification device, a centrifugal machine and a recovery tank, wherein the centrifugal machine is communicated with a circulation tank which is communicated with the pre-separation tank; the pre-separation tank is communicated with a separation liquid inlet pipe, and the separation liquid inlet pipe and the circulating tank respectively extend into the bottom of the pre-separation tank through corresponding insertion pipes; a first baffle and a second baffle are arranged in the pre-separation tank, the first baffle is close to the position of the insertion pipe, and the second baffle is close to one side of the heavy component aggregation package; the pre-separation tank is communicated with the heavy component collecting tank through a siphon.
2. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the first baffle comprises an upper plate and a lower plate, wherein the upper plate is of a non-porous plate structure, and the lower plate is of a porous plate structure.
3. The non-stationary feed partially emulsified liquid-liquid two phase separation system according to claim 1 or 2 wherein: the second baffle is of a non-porous plate structure.
4. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 2, wherein: the upper plate and the lower plate are connected by bolts.
5. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the collecting tank comprises a light component collecting tank and a heavy component collecting tank, and the light component collecting tank and the heavy component collecting tank are provided with or without stirring devices; the pre-separation tank is respectively communicated with a light component collecting tank and a heavy component collecting tank, the light component collecting tank or the heavy component collecting tank is communicated with an extrusion demulsification device, the extrusion demulsification device is communicated with a centrifugal machine, and the centrifugal machine is communicated with a recovery tank; the heavy component collecting tank or the light component collecting tank is communicated with the circulating tank; the light component collecting tank or the heavy component collecting tank and the recovery tank are respectively communicated with a system recovery device; the centrifugal machine is communicated with the centrifugal machine slag tank.
6. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the collecting tank comprises a light component collecting tank and a heavy component collecting tank, and stirrers are arranged in the light component collecting tank and the heavy component collecting tank; the pre-separation tank is respectively communicated with a light component collecting tank and a heavy component collecting tank, the light component collecting tank is communicated with a first extrusion demulsification device, the first extrusion demulsification device is communicated with a first centrifugal machine, and the first centrifugal machine is communicated with a first recovery tank; the heavy component collecting tank is communicated with a second extrusion demulsification device, the second extrusion demulsification device is communicated with a second centrifugal machine, and the second centrifugal machine is communicated with a second recovery tank; the first centrifugal machine and the second centrifugal machine are respectively communicated with the circulating tank; the light component collecting tank, the first recovery tank, the heavy component collecting tank and the second recovery tank are respectively communicated with a system recovery device; the centrifugal machine is communicated with the centrifugal machine slag tank.
7. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the corresponding insertion pipes of the circulation tank and the corresponding insertion pipes of the separation liquid inlet pipe are arranged in parallel along the longitudinal direction.
8. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the centrifuge is internally provided with a specific gravity ring, and the inner diameter of the specific gravity ring is controlled to be 90-110 mm.
9. The non-stationary feed partially emulsified liquid-liquid two phase separation system as set forth in claim 1, wherein: the pre-separation tank is of a horizontal tank structure, the collection tank is of a vertical tank structure, and the centrifuge is a three-phase centrifuge.
10. The non-steady state feed partially emulsified liquid-liquid two phase separation system as set forth in claim 5 or 6, wherein: and a corresponding tank bottom inlet pipe orifice is reserved at the top of the light component collecting tank with stirring and the heavy component collecting tank with stirring.
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| CN202020837154.7U CN212236086U (en) | 2020-05-19 | 2020-05-19 | Unsteady-state feeding part emulsified liquid-liquid two-phase separation system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111437629A (en) * | 2020-05-19 | 2020-07-24 | 浙江众立合成材料科技股份有限公司 | Unsteady-state feeding partial-emulsification liquid-liquid two-phase separation system and application |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111437629A (en) * | 2020-05-19 | 2020-07-24 | 浙江众立合成材料科技股份有限公司 | Unsteady-state feeding partial-emulsification liquid-liquid two-phase separation system and application |
| CN111437629B (en) * | 2020-05-19 | 2023-08-04 | 浙江众立合成材料科技股份有限公司 | Liquid-liquid two-phase separation system for emulsification of unsteady-state feeding part and application |
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