CN113816460B - Self-overflow iterative separation cyclone and application thereof in separation of DNAs PLS in underground water - Google Patents
Self-overflow iterative separation cyclone and application thereof in separation of DNAs PLS in underground water Download PDFInfo
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- CN113816460B CN113816460B CN202111199336.1A CN202111199336A CN113816460B CN 113816460 B CN113816460 B CN 113816460B CN 202111199336 A CN202111199336 A CN 202111199336A CN 113816460 B CN113816460 B CN 113816460B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
Abstract
The present disclosure relates to a self-overflow iterative separation cyclone and its application in separation of DNAPLs in groundwater, providing a self-overflow iterative separation cyclone comprising: cylinder section (1), circular cone section (2), underflow pipe (3), interior overflow pipe (4), latus rectum overflow pipe (5), coalescence breakdown of emulsion bifidobacterium pipe import (6), interior overflow pipe outfall (7), latus rectum overflow pipe outfall (8), underflow opening (9) and overflow drainage venturi, wherein, overflow drainage venturi includes: the venturi tube comprises a front venturi tube section (10), a reducing section (11), a throat section (12), a gradually expanding section (13), a rear venturi tube section (14) and a throat return pipe (15). Also provides an application of the self-overflow iterative separation cyclone in the separation of DNAs and PLs in underground water.
Description
Technical Field
The disclosure belongs to the technical field of cyclone separation, and relates to a self-overflow iterative liquid-liquid hydrocyclone which is suitable for separating heavy non-aqueous phase liquids (DNAs) from water in polluted underground water. Specifically, the disclosure provides a self-overflow iterative separation cyclone and application thereof in separation of DNAs PLs in underground water.
Background
In recent years, with the rapid development of industrial processes in China, the problems of heavy non-aqueous phase pollution caused by leakage and discharge of coal tar, heavy mineral oil and the like generated in industrial links such as mineral exploitation, metal smelting, petrochemical industry and the like, biological medicines, halogenated solvents widely applied in basic production and extracting agents are increasingly aggravated, and the pollution is a leading factor of soil and underground water. Such contaminants are generally denser than water, easily penetrate soil into groundwater, and form DNAPLs, which are persistent sources of contamination and cause serious "triple-cause" (carcinogenic, teratogenic, mutagenic) hazards to human health.
DNAPLs are not easy to dissolve in water, have high viscosity, are easy to emulsify, have density heavier than water, and have weak mobility, difficult degradability and low water solubility, and can finally stay at the bottom of an aquifer through the aquifer in the underground water transportation process and are extremely unevenly distributed. For the separation of DNAPLS pollutants in underground water, the traditional single separation method, namely a cyclone separation method, a coalescence separation method, a membrane separation method and the like, cannot achieve efficient and rapid separation. The high-speed rotating shearing flow field in the cyclone can intensify the emulsification of the DNAPLs, so that the high-efficiency separation of small-particle-size liquid drops cannot be ensured, and the separation efficiency is reduced; the coalescence-separation equipment occupies a large area, and the free state stays in the separation bed layer for too long and discontinuously, so that the separation efficiency is low; the membrane separation method has high cost, and the separation process is easy to block, so the method is not suitable for the separation. Therefore, in the groundwater pollution remediation problem which is to be solved at present, it is important to develop and improve a new technology and a new device for separating DNAPLs in groundwater.
For liquid-liquid cyclone separation, researchers have improved the structure of a hydrocyclone more. In order to improve the separation efficiency, a mode of connecting a plurality of stages of hydrocyclones in series or changing the structure of a component of the hydrocyclone in series with other separation equipment is generally adopted. This not only increases the manufacturing cost and the operation and maintenance cost, but also increases the installation workload and the installation space.
US20060130444a1 describes a separation device with a plurality of hydrocyclones connected in series, the overflow of each separation stage being connected to the inlet of the next separation stage for a secondary separation. Similarly, CN208912333U provides a multistage hydrocyclone separation device, which comprises at least two first-stage hydrocyclones connected in series, the first outlets of the second-stage hydrocyclones are respectively connected to the first outlets of the corresponding first-stage hydrocyclones, and the second outlets of the second-stage hydrocyclones are both connected to a settling separator, which has the advantages of good separation effect and large treatment capacity, but the device has large floor area, multiple equipment structures and high manufacturing cost, and the substances to be separated stay in the device for a long time, and is not suitable for the environment with limited space, and cannot meet the requirement of rapid separation.
US20200122163a1 describes a hydrocyclone and a multiple combined hydrocyclone system, which cyclone has a drain arranged at the upper part of the column section, separate from the overflow pipe, which effectively reduces the risk of the coarse fraction being misplaced and left in the column section, reduces maintenance requirements and prolongs the service life of the hydrocyclone, but the structure of which affects the stability of the hydrocyclone plant and reduces the separation efficiency.
WO0141934a1 discloses a recirculation cyclone for dust removal and dry gas purification, comprising a counter-flow cyclone collector and a straight-through cyclone concentrator, wherein relatively clean substances flowing out of the counter-flow cyclone collector enter the straight-through cyclone concentrator for secondary separation, light-phase substances are discharged after the secondary separation, and heavy-phase substances enter the counter-flow cyclone collector for further separation.
CN203124134U discloses a novel adjustable concentric two overflow pipe formula three product hydrocyclones, its characterized in that overflow pipe inboard overflow pipe and outside overflow pipe, accessible change in, outside overflow pipe diameter size, outside overflow pipe depth of insertion improve the swirler classification performance, can the product of three kinds of different particle sizes of simultaneous separation, have compact structure, application scope is wide, the high advantage of operation elasticity, but this device can not carry out the secondary separation to the looks material, lead to the shortcoming that separation efficiency is low.
CN104773788A discloses a circulating cyclone separator, which is characterized in that cleaner water after cyclone separation in an internal and external circulating pipeline systems rises from an internal circulating pipe, is sucked into a water pump through an external circulating pipe, and then enters a cyclone from a water inlet pipe through the water pump to perform secondary separation.
CN111686950A discloses a method and device for quickly separating oil and water under high temperature and high pressure, which includes a first-stage separation upper shell provided with a hydrocyclone and a second-stage separation lower shell provided with a coalescer, the upper shell is provided with an overflow liquid outlet and an underflow liquid outlet which can be respectively connected with an overflow liquid return port and an underflow liquid return port arranged on the top of the lower shell through pipes, the method and device have the advantages of improving the high temperature and high pressure resistance of the hydrocyclone by changing the connection position of the external interfaces of the upper shell and the lower shell, realizing the quick separation of oil and water in one device, and improving the separation efficiency, but the device has larger structure floor area, and is not suitable for places with limited installation space.
CN109332018A discloses a hydrocyclone, which is characterized in that a plurality of baffles are arranged in the liquid inlet pipe of the hydrocyclone, so that the contact area of two phases can be increased, the turbulent energy can be increased, and the hydrocyclone has the characteristics of extraction and separation capabilities, but the pressure drop of the pipeline is increased, so that the disadvantages of dispersed phase emulsification, unstable flow field and separation efficiency reduction can be caused.
In conclusion, in the liquid-liquid cyclone separation process, the problem of low separation efficiency caused by more circulating flow and short-circuit flow in the cyclone also exists; dispersion phase emulsification problems; the problems of rotational flow center offset and short-circuit flow increase caused by unstable flow field; the single equipment has low separation efficiency, large occupied area of multi-stage series-parallel connection and the like. Aiming at the underground water separation process containing DNAPLS, a hydrocyclone which has the advantages of simple structure, high efficiency, rapid two-phase separation, minimized occupied space, high classification precision, high separation efficiency, low energy consumption and demulsification is urgently needed to be developed.
Disclosure of Invention
The present disclosure provides a novel hydrocyclone capable of guiding short-circuit flow to perform iterative separation and separating emulsified dispersed phase, so as to better solve the problem of low separation efficiency of the existing liquid-liquid separation hydrocyclone.
In one aspect, the present disclosure provides a self-overflow iterative separation cyclone, comprising: cylinder section, cone section, underflow pipe, interior overflow pipe, latus rectum overflow pipe, coalescence breakdown of emulsion double manifold import, interior overflow pipe outfall, latus rectum overflow pipe outfall, underflow opening and overflow drainage venturi, wherein, overflow drainage venturi includes: the Venturi tube front section, the reducing section, the throat part, the gradually expanding section, the Venturi tube rear section and the throat part return pipe; the coalescence demulsification bifidotube is connected with the outer circumference of the upper end of the cylindrical section in a horizontal tangential manner, the lower end of the cylindrical section is connected with the upper end of the cylindrical section, the lower end of the conical section is connected with the upper end of an underflow pipe, a drift diameter overflow pipe is positioned in the cylindrical section, an inner overflow pipe is positioned in the drift diameter overflow pipe, the central axes of the drift diameter overflow pipe and the inner overflow pipe are coincided with the central axis of the cylindrical section, the lower end of the inner overflow pipe is positioned between the upper part of the conical section and the lower part of the drift diameter overflow pipe, the drift diameter overflow pipe is vertical to the axis of a flow outlet of the drift diameter overflow pipe, the drift diameter overflow pipe is positioned above the cylindrical section, the drift diameter overflow pipe is connected with a backflow pipe of a throat of an overflow drainage venturi, the inner overflow pipe is coaxial with the flow outlet of the inner overflow pipe, the flow outlet of the inner overflow pipe is positioned above the drift diameter overflow pipe, and the rear section of the venturi is connected with the coalescence demulsification bifidotube; the central axes of other parts of the overflow drainage Venturi tube except the throat return tube are coincident.
In a preferred embodiment, the coalescence demulsification bifido pipe is filled with lipophilic and hydrophobic coalescence material inside and has equal branch pipe length.
In another preferred embodiment, the drift diameter overflow pipe outlet pipe is connected with the outer circumference of the drift diameter overflow pipe in a horizontal tangential direction, and the drift diameter overflow pipe outlet is connected with the overflow drainage Venturi throat return pipe.
In another preferred embodiment, the height of the cylindrical section is 1.2-2 times the diameter of the cylindrical section, the diameter of the drift tube is 0.6-0.8 times the diameter of the cylindrical section, the diameters of the internal overflow tube and the underflow tube are 0.2-0.5 times the diameter of the cylindrical section, and the cone angle of the conical section is between 1.5-6 °.
In another preferred embodiment, the depth of insertion of the internal overflow tube into the cylindrical section is from 0.4 to 0.9 times the diameter of the cylindrical section and the depth of insertion of the drift diameter overflow tube into the cylindrical section is from 0.4 to 1.5 times the depth of insertion of the internal overflow tube into the cylindrical section.
In another preferred embodiment, the installation angle of the cyclone, i.e. the central axes of the cylindrical section, the conical section, the underflow pipe, the inner overflow pipe and the drift diameter overflow pipe, is between 0 and 90 ° from the horizontal.
In another preferred embodiment, the installation angle of the overflow drainage Venturi tube, namely the included angle between the central axes of the front section, the reducing section, the throat part, the diverging section and the rear section of the Venturi tube and the central axis of the swirler is 0-90 degrees.
In another aspect, the present disclosure provides the use of the above-described self-overflow iterative separation cyclone for the separation of DNAPLs in groundwater, wherein the cyclones are used individually or in parallel.
In a preferred embodiment, a plurality of cyclones are installed in a pressure-bearing tank body, and the central axes of the cyclones are parallel to the axis of the pressure-bearing tank body; a partition plate is arranged in the pressure-bearing tank body and used for fixing the cyclone and dividing the liquid phase storage volume; the pressure-bearing tank body is provided with a mixed liquid inlet, a light phase outlet and a heavy phase outlet.
In another preferred embodiment, the cyclone is mounted in the opposite direction to the pressure-containing tank.
Has the advantages that:
the invention can realize multi-stage high-efficiency iterative separation in one cyclone, and compared with the common cyclone, the invention has the following advantages:
(1) a self-flooding iterative system. The top of the cyclone is coaxially provided with a drift diameter overflow pipe which is connected with a return pipe at the throat part of the Venturi tube, so that the materials in the middle transition zone in the cyclone can automatically flow back to enter the cyclone for iterative separation, and the drift diameter overflow structure can effectively shorten the radial movement distance of the light-phase materials and is favorable for conducting drainage short-circuit flow for iterative separation.
(2) And a coalescence demulsification inlet pipe. The inlet pipeline is filled with oleophylic and hydrophobic agglomeration materials, so that the mixed solution of emulsified dispersed phases can be demulsified and then quickly separated by cyclone; meanwhile, the middle phase substance reflowing through the path overflow pipe can accelerate the growth process of dispersed phase droplets, thereby improving the separation efficiency.
(3) And the bifidus pipes are arranged at equal intervals. The branch pipes of the double manifolds are equal in length, so that the pressure drop borne by the inlet pipe is the same, and the stable swirling flow field is generated.
(4) And (4) industrial application of flip-chip sedimentation. In the application of the self-overflow iterative separation cyclone in the separation of DNAs and PLs in underground water, a plurality of self-overflow iterative separation cyclones can be installed in the pressure-bearing tank body, and the cyclones and the tank body are installed in opposite directions to carry out sedimentation separation, so that the separation efficiency is improved.
Drawings
The accompanying drawings are included to provide a further understanding of the disclosure, and are incorporated in and constitute a part of this specification to further illustrate the disclosure and not limit the disclosure.
Fig. 1 is a schematic view of the overall structure of a self-overflowing iterative separation cyclone according to a preferred embodiment of the present disclosure.
FIG. 2 is a longitudinal sectional view of a self-overflowing iterative separation cyclone structure according to a preferred embodiment of the present disclosure.
FIG. 3 is a top view of the overall structure of a self-overflowing iterative separation cyclone, according to a preferred embodiment of the present disclosure.
Fig. 4 is a schematic diagram of a coalesced demulsifying bifidotube inlet material fill in accordance with a preferred embodiment of the present disclosure.
FIG. 5 is a schematic diagram of an integrated industrial application of a self-overflowing iterative separation cyclone according to a preferred embodiment of the present disclosure.
FIG. 6 is a schematic diagram of an integrated industrial application of a self-overflowing iterative separation cyclone according to a preferred embodiment of the present disclosure.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
After extensive and intensive research, the applicant of the invention finds that the traditional cyclone separator has a small structure, is simple to operate, has large treatment capacity and high separation efficiency, but has general separation and purification effects on dispersed phase, emulsified liquid droplets and other small-particle-size liquid droplets, and the high-efficiency separation is difficult to ensure; the coalescence-separation only changes the particle size distribution state of dispersed phase droplets through the process of making small droplets collide or wet and coalesce into large droplets, does not reduce the dispersed phase concentration, does not need to add chemical agents, but has the problems of long residence time of the dispersed phase droplets, large required space and discontinuous separation; by combining the characteristics of complicated underground heavy non-aqueous phase forms, instability, difficult separation and easy emulsification, if the heavy non-aqueous phase liquid with small particle size in the mixed medium is coalesced into larger liquid drops before entering the cyclone or the middle phase substance in the middle transition zone in the cyclone can be guided into the same structure for circular separation without external work, the separation and purification effects of the cyclone separator can be further improved; based on the purposes and the principles, by analyzing the distribution rules of the flow fields in the cyclone and the coalescer and the distribution characteristics of the particle sizes of liquid drops and combining experimental research, the coupling of cyclone separation and coalescence separation can effectively separate underground heavy nonaqueous phase liquid. Based on the above findings, the present invention has been completed.
The technical concept of the invention is as follows:
the top of the cyclone is coaxially provided with a drift diameter overflow pipe, and the inlet of the cyclone is provided with an overflow drainage Venturi pipe and an inlet of a coalescence demulsification bifido pipe; after the liquid-liquid mixed phase containing the water heavy non-aqueous phase enters a self-overflow iterative separation cyclone, the concentration of the heavy non-aqueous phase liquid shows a trend of high periphery and low middle under the action of centrifugal force, the heavy non-aqueous phase mixture in a middle transition zone is led out to a drainage Venturi tube through a drift diameter overflow pipe, the heavy non-aqueous phase is coalesced through a coalescence demulsification bifidotube and then enters the cyclone for iterative separation, and the aqueous phase in a central clarification zone is led out through the drift diameter overflow pipe, so that the deep purification of the aqueous phase and the enrichment dehydration of the heavy non-aqueous phase are realized. The self-overflow iterative separation cyclone can meet the requirement of large treatment capacity by integrating parallel connection, is suitable for liquid-liquid separation of a water phase containing a second phase such as a free state, an emulsified state and the like, such as separation of a water-containing heavy non-water phase in oil-containing sewage and underground water remediation industries generated in oil field produced water or coal chemical industry, and has the advantages of capability of effectively reducing iterative separation of circulating flow and drainage short-circuit flow in the cyclone, good separation effect, high efficiency, convenience in installation, compact structure, convenience in operation and maintenance and the like.
In a first aspect of the present disclosure, there is provided a self-overflowing iterative separation cyclone comprising: cylinder section, cone section, underflow pipe, interior overflow pipe, latus rectum overflow pipe, coalescence breakdown of emulsion double manifold import, interior overflow pipe outfall, latus rectum overflow pipe outfall, underflow opening and overflow drainage venturi, wherein, overflow drainage venturi includes: the front section, the reducing section, the throat part, the gradually expanding section, the rear section and the throat part of the Venturi tube are respectively provided with a Venturi tube; the coalescence demulsification bifidotube is connected with the outer circumference of the upper end of the cylindrical section in a horizontal tangential manner, the lower end of the cylindrical section is connected with the upper end of the cylindrical section, the lower end of the conical section is connected with the upper end of an underflow pipe, a drift diameter overflow pipe is positioned in the cylindrical section, an inner overflow pipe is positioned in the drift diameter overflow pipe, the central axes of the drift diameter overflow pipe and the inner overflow pipe are coincided with the central axis of the cylindrical section, the lower end of the inner overflow pipe is positioned between the upper part of the conical section and the lower part of the drift diameter overflow pipe, the drift diameter overflow pipe is vertical to the axis of a flow outlet of the drift diameter overflow pipe, the drift diameter overflow pipe is positioned above the cylindrical section, the drift diameter overflow pipe is connected with a backflow pipe of a throat of an overflow drainage venturi, the inner overflow pipe is coaxial with the flow outlet of the inner overflow pipe, the flow outlet of the inner overflow pipe is positioned above the drift diameter overflow pipe, and the rear section of the venturi is connected with the coalescence demulsification bifidotube; the central axes of other parts of the overflow drainage Venturi tube except the throat return tube are coincident.
In the disclosure, the inlet of the coalescence demulsification bifidotube is connected with the outer circumference of the cylindrical section in a horizontal tangential manner, oleophylic and hydrophobic agglomeration materials are filled in the bifidotube pipeline, and the branch pipelines of the double manifolds have equal lengths.
In this disclosure, latus rectum overflow pipe outflow pipe is the horizontal tangential with latus rectum overflow pipe outer circumference and is connected, and latus rectum overflow pipe outfall is connected with venturi throat back flow.
In the disclosure, the height of the cylindrical section of the cyclone is 1.2-2 times of the diameter of the cylindrical section, the diameter of the drift diameter overflow pipe is 0.6-0.8 times of the diameter of the cylindrical section, the diameters of the inner overflow pipe and the underflow pipe are 0.2-0.5 times of the diameter of the cylindrical section, and the cone angle of the conical section is 1.5-6 degrees.
In the disclosure, the depth of the internal overflow pipe inserted into the cylindrical section is 0.4-0.9 times the diameter of the cylindrical section, and the depth of the drift diameter overflow pipe inserted into the cylindrical section is 0.4-1.5 times the depth of the internal overflow pipe inserted into the cylindrical section.
In the present disclosure, the mounting angle of the swirler, i.e., the central axes of the cylindrical section, the conical section, the underflow pipe, the inner overflow pipe and the drift diameter overflow pipe, is between 0 and 90 degrees from the horizontal.
In the present disclosure, the installation angle of the venturi tube, i.e. the included angle between the central axis of the front section, the reducing section, the throat part, the expanding section and the rear section of the venturi tube and the central axis of the swirler is between 0 and 90 degrees.
In a second aspect of the disclosure, an application of the self-overflow iterative separation cyclone in separation of DNAPLs in groundwater is provided, which is suitable for integrated industrial application of liquid-liquid separation, such as separation of heavy non-aqueous phase pollution source and water in oil field production water or oily sewage generated in coal chemical industry.
In the present disclosure, the cyclones are not limited to a single application and may be installed in parallel.
In the disclosure, a plurality of cyclones are installed in a pressure-bearing tank body, and the central axes of the cyclones are parallel to the axis of the tank body; a partition plate is arranged in the pressure-bearing tank body and used for fixing the cyclone and dividing the liquid phase storage volume; the tank body is provided with a mixed liquid inlet, a light phase outlet and a heavy phase outlet.
In the present disclosure, a plurality of self-overflowing iterative separation cyclones are mounted in a tank body in a direction opposite to a tank body direction.
The working principle of the invention is as follows: when the cyclone separator works, mixed liquid to be separated enters the venturi tube from the front section of the venturi tube, the flow velocity is increased in the reducing section of the venturi tube, the mixed liquid passes through the throat part and the gradually expanding section, flows through the inlet of the coalescence demulsification bifidotube, enters the cylindrical section of the cyclone, rotates at a high speed along the inner wall of the cylindrical section, the two phases in the mixed liquid have different densities, the two phases begin to be separated under the action of centrifugal force, the phase with the higher density gradually reaches the side wall of the cyclone along the radial direction under the action of a rotating flow field, moves downwards along the axial direction to form an outer rotational flow, finally flows through the underflow tube and is discharged from an underflow port; the lower-density one phase moves towards the central axis direction of the swirler to form an inner vortex, and a dispersed phase is crushed and coalesced due to the strong vortex action of a flow field, so that the separation effects at different radial positions of the inner vortex are different, light-phase substances near the central axis of the swirler are discharged from the outlet of the inner overflow pipe along the inner overflow pipe, and middle-phase substances in the intermediate transition zone are led out to the throat return pipe of the venturi pipe through the radial overflow pipe under the suction action of negative pressure generated by the vortex flow field and the throat of the venturi pipe and enter the venturi pipe, and a coalescence demulsification double manifold enters the hydrocyclone again along with mixed liquid to perform iterative separation, thereby realizing deep purification of a water phase and enrichment dehydration of a second phase.
Reference is made to the accompanying drawings.
Fig. 1 is a schematic view of the overall structure of a self-overflowing iterative separation cyclone according to a preferred embodiment of the present disclosure. As shown in fig. 1, the self-overflowing iterative separation cyclone includes: cylindrical section 1, circular cone section 2, underflow pipe 3, interior overflow pipe 4, latus rectum overflow pipe 5, coalescence breakdown of emulsion bimanifold import 6, interior overflow pipe outfall 7, latus rectum overflow pipe outfall 8, underflow opening 9 and overflow drainage venturi, wherein, overflow drainage venturi includes: a front section 10 of the Venturi tube, a reducing section 11, a throat part 12, a gradually expanding section 13, a rear section 14 of the Venturi tube and a throat part return pipe 15; the coalescence demulsification bifido tube is connected with the upper end outer circumference of the cylindrical section in a horizontal tangential manner, the lower end of the cylindrical section is connected with the upper end of the cylindrical section, the lower end of the cylindrical section is connected with the upper end of an underflow pipe, a drift diameter overflow pipe is positioned in the cylindrical section, an inner overflow pipe is positioned in the drift diameter overflow pipe, the central axes of the drift diameter overflow pipe and the inner overflow pipe are coincided with the central axis of the cylindrical section, the lower end of the inner overflow pipe is positioned between the upper part of the conical section and the lower part of the drift diameter overflow pipe, the drift diameter overflow pipe is vertical to the axis of a flow outlet of the drift diameter overflow pipe, the drift diameter overflow pipe is positioned above the cylindrical section, the drift diameter overflow pipe is connected with an overflow drainage Venturi return pipe, the inner overflow pipe is coaxial with the flow outlet of the inner overflow pipe, the flow outlet of the inner overflow pipe is positioned above the drift diameter overflow pipe, and the rear section of the Venturi is connected with the coalescence demulsification bifido tube; the central axes of other parts of the overflow drainage Venturi tube except the throat return tube are coincident.
FIG. 2 is an axial cross-sectional view of a self-overflowing iterative separation cyclone structure according to a preferred embodiment of the present disclosure. As shown in fig. 2, the self-overflowing iterative separation cyclone comprises: cylindrical section 1, circular cone section 2, underflow pipe 3, interior overflow pipe 4, latus rectum overflow pipe 5, coalescence breakdown of emulsion bimanifold import 6, interior overflow pipe outfall 7, latus rectum overflow pipe outfall 8, underflow port 9 and overflow drainage venturi, the coaxial latus rectum overflow pipe that sets up in swirler top, wherein, Do represents interior overflow pipe diameter, Dn represents cylindrical section diameter, Dt represents latus rectum overflow pipe diameter, Du represents the underflow pipe diameter, alpha represents the cylinder section tapering, H represents the cylinder section height, H represents the cylinder section height 1 Indicates the depth of insertion of the inner downcomer, h 2 Indicating the depth of insertion through the downcomer, a and b indicating the inlet cross-sectional dimensions, and Lu indicating the length of the underflow tube.
FIG. 3 is a top view of the overall structure of a self-overflowing iterative separation cyclone, according to a preferred embodiment of the present disclosure. As shown in fig. 3, the self-overflowing iterative separation cyclone comprises: cylindrical section 1, cone section, underflow pipe, interior overflow pipe 4, latus rectum overflow pipe 5, coalescence breakdown of emulsion bimanifold import 6, interior overflow pipe outfall 7, latus rectum overflow pipe outfall 8, underflow opening and overflow drainage venturi, wherein, overflow drainage venturi includes: a front section 10 of the Venturi tube, a reducing section 11, a throat part, a gradually expanding section 13, a rear section 14 of the Venturi tube and a throat part return pipe 15; an overflow drainage Venturi tube and an inlet of a coalescence demulsification bifidotube are arranged at the inlet of the cyclone, a return pipe 15 at the throat part of the Venturi tube is connected with an outlet 8 of a drift diameter overflow pipe, the drift diameter overflow pipe is used for draining medium substances in a middle transition zone, the medium substances are led out to the drainage Venturi tube through the drift diameter overflow pipe, and a coalescence heavy phase flows through the coalescence demulsification bifidotube and then enters the cyclone for iterative separation, so that the separation precision and efficiency are improved; the cyclone inlet is a coalescence demulsification double-manifold inlet which is connected with the outer circumference of the cylindrical section in a horizontal tangential manner, the branch pipelines of the bifidus pipes are equal in length, and the lengths of the two inlet pipelines entering the cyclone from the rear section of the Venturi pipe are equal to ensure that the pressure drop of the mixed liquid entering the cyclone through the two pipelines is the same, so that a symmetrical and stable cyclone field is generated, and the separation efficiency is improved.
Fig. 4 is a schematic filling diagram of a coalescing demulsification bifidotube inlet material according to a preferred embodiment of the present disclosure. As shown in fig. 4, the line a-a is an inlet of a coalescence demulsification bifidus tube, the pipeline of the inlet of the coalescence demulsification bifidus tube is filled with oleophylic and hydrophobic agglomeration materials, dispersed phase droplets in the mixed solution gradually grow up under the interception and collision action of the agglomeration materials, the agglomerated phase droplets are separated from the dispersed phase droplets and enter a cyclone, the dispersed phase droplets are separated under the action of centrifugal force, heavy phase substances are discharged from a bottom flow port, light phase substances are discharged from an inner overflow pipe, and the middle phase substances enter the cyclone through a throat backflow pipe and the coalescence demulsification bifidus tube again under the suction action of negative pressure generated by a vortex field and the throat of a venturi tube; when the coalescence material flows through the inlet pipeline, the dispersed phase drops in the middle phase substance are adhered to the material, so that the growth and the separation of the drops on the coalescence material are accelerated, and the two-phase separation is facilitated.
FIG. 5 is a schematic diagram of an integrated industrial application of a self-overflowing iterative separation cyclone according to a preferred embodiment of the present disclosure. As shown in fig. 5, four self-overflow iterative separation cyclones are installed in the separation tank 19, and the installation direction of the cyclones is the same as the direction of the tank body; the self-overflow iterative separation cyclone is arranged in the tank body of the separation tank 19, and the central axis of the cyclone is parallel to the axis of the tank body; a clapboard 16 is arranged in the tank body and used for fixing the cyclone and dividing the liquid phase storage volume, and a sealing gasket is arranged between the clapboard and the pipeline of the cyclone for fixation; the tank body is provided with a mixed liquid inlet 18, a light phase outlet 17 and a heavy phase outlet 20.
FIG. 6 is a schematic diagram of an integrated industrial application of a self-overflowing iterative separation cyclone, according to a preferred embodiment of the present disclosure. As shown in fig. 6, four self-overflow iterative separation cyclones are installed in the separation tank 19 in the direction opposite to the tank direction; the self-overflow iterative separation cyclone is arranged in the tank body of the separation tank 19, and the central axis of the cyclone is parallel to the axis of the tank body; a clapboard 16 is arranged in the tank body and used for fixing the cyclone and dividing the liquid phase storage volume, and a sealing gasket is arranged between the clapboard and the pipeline of the cyclone for fixation; the tank body is provided with a mixed liquid inlet 18, a light phase outlet 17 and a heavy phase outlet 20.
Examples
The invention is further illustrated below with reference to specific examples. It is to be understood, however, that these examples are illustrative only and are not to be construed as limiting the scope of the present invention. Test methods in which specific conditions are not specified in the following examples are generally carried out under conventional conditions or under conditions recommended by the manufacturer. All percentages and parts are by weight unless otherwise indicated.
Example 1:
in this embodiment, the self-overflow iterative separation cyclone is integrated and applied to the separation of oily sewage, and an industrial device is shown in fig. 5.
1. Equipment structure
As shown in fig. 5.
2. Structural dimensions
As shown in table 1 below and fig. 2.
TABLE 1 cyclone structural dimensions
| (symbol) | Physical significance | Unit of | Numerical value | |
| D n | Diameter of cylindrical section | mm | 35 | |
| H | Height of cylindrical section | mm | 1.2D n | |
| L u | Length of underflow pipe | mm | 0.64D n | |
| D o | Diameter of inner overflow pipe | mm | 0.24D n | |
| D t | Diameter of drift diameter overflow pipe | mm | 0.34D n | |
| D u | Diameter of underflow pipe | mm | 0.24D n | |
| axb | Inlet | mm | 6×8 | |
| h 1 | Depth of insertion of internal overflow tube | mm | 0.618D n | |
| H 2 | Depth of insertion of drift diameter overflow pipe | mm | 0.618h 1 | |
| α | Taper of cylindrical section | ° | 2 |
3. Operating conditions
As shown in table 2 below.
TABLE 2 operating conditions of an integrated application of a self-overflow iterative separation cyclone to an oily sewage separation device
| Operating conditions | Numerical value | Unit of |
| Pressure of | 0.3-1 | MPa |
| Temperature of | 20-35 | ℃ |
| Extent of treatment | 0.4-1.4 | m 3 /h |
| Oil content ratio | 1-50 | ％ |
4. Process flow
The oily sewage enters a separation tank through a mixed liquid inlet, enters a Venturi tube under the action of pressure, enters a swirler through a coalescence demulsification bifidotube inlet after being accelerated in the Venturi tube, two phases begin to be separated under the action of centrifugal force, a water phase with higher density gradually reaches the side wall of the swirler along the radial direction under the action of a rotating flow field, moves downwards along the axial direction at the same time, is discharged to a heavy phase area of the separation tank through a underflow port and is discharged through a heavy phase outlet; the oil with lower density moves towards the central axis direction of the swirler, cleaner oil phase substances near the central axis of the swirler enter a light phase area along an inner overflow pipe and are discharged from a light phase outlet; and the oil-water mixture in the intermediate transition zone is led out to the throat part of the Venturi tube through the radial overflow pipe under the suction action of the negative pressure generated by the vortex flow field and the throat part of the Venturi tube, enters the coalescence demulsification double-manifold pipe along with the mixed liquid, enters the hydrocyclone again for iterative separation, and realizes the deep purification of the water phase and the enrichment dehydration of the oil phase.
5. Effects of the implementation
The oily sewage separation test is carried out by simulating oily sewage by using tap water and diesel oil (5 percent, volume concentration) and the test temperature is 25 ℃. The physical properties of the diesel oil and water used are shown in Table 3 below, and the results of the experiment are shown in Table 4 below.
TABLE 3 physical Property parameters
| Material(s) | Density/(kg/m) 3 ) | Kinematic viscosity/(kg/m.s) |
| Water (W) | 998.2 | 0.001003 |
| Diesel oil | 852.75 | 0.33 |
TABLE 4 results of oily water separation experiments
| Flow/(m) 3 /h) | Separation efficiency/%) | Oil phase water content% |
| 0.4 | 95.28 | 0.93 |
| 0.6 | 95.69 | 0.87 |
| 0.8 | 96.57 | 0.69 |
| 1.0 | 97.23 | 0.61 |
| 1.2 | 96.51 | 0.67 |
| 1.4 | 95.91 | 0.81 |
According to experimental results, the separation efficiency of the device on the oily sewage is more than 95%, and the water content of the separated oil phase is less than 1%.
Example 2:
in this embodiment, the self-overflow iterative separation cyclone is integrated and applied to enrichment and dehydration of underground heavy non-aqueous phase pollution sources, and after separation, the water content of the heavy non-aqueous phase is less than 10%, and an industrial device is shown in fig. 6.
1. Equipment structure
As shown in fig. 6.
2. Structural dimensions
As shown in table 5 below and fig. 2.
TABLE 5 cyclone structural dimensions
| (symbol) | Physical significance | Unit of | Numerical value | |
| D n | Diameter of cylindrical section | mm | 25 | |
| H | Height of cylindrical section | mm | 1.2D n | |
| L u | Length of underflow pipe | mm | 0.64D n | |
| D o | Diameter of inner overflow pipe | mm | 0.24D n | |
| D t | Diameter of drift diameter overflow pipe | mm | 0.34D n | |
| D u | Diameter of underflow pipe | mm | 0.24D n | |
| axb | Inlet | mm | 3×4 | |
| h 1 | Depth of insertion of internal overflow tube | mm | 0.618D n | |
| H 2 | Depth of insertion of drift diameter overflow pipe | mm | 0.618h 1 | |
| α | Taper of cylindrical section | ° | 2 |
3. Operating conditions
Same as in example 1.
4. Process flow
Underground water containing heavy non-aqueous phase liquid enters a separation tank through a mixed liquid inlet, enters a Venturi tube under the action of pressure, enters a cyclone through a coalescence demulsification bifidotube inlet after being accelerated in the Venturi tube, two phases begin to be separated under the action of centrifugal force, the heavy non-aqueous phase with higher density gradually reaches the side wall of the cyclone along the radial direction under the action of a rotating flow field, moves upwards along the axial direction at the same time, is discharged to a heavy phase area of the separation tank through a bottom flow port, and is discharged through a heavy phase outlet at the lower part of the heavy phase area after being settled and separated; the water phase with lower density moves towards the central axis direction of the cyclone, and the cleaner water phase near the central axis of the cyclone enters a light phase area along an inner overflow pipe and is discharged from a light phase outlet; and the mixture of the heavy non-aqueous phase liquid and water in the intermediate transition zone is led out to a venturi tube throat return pipe through a radial overflow pipe under the suction action of a vortex flow field and negative pressure generated at the venturi tube throat to enter a venturi tube and a coalescence demulsification double manifold, and under the coalescence action of materials in a double-manifold, the heavy non-aqueous phase liquid is accelerated to grow and separated from the materials, and the separated materials enter a hydraulic cyclone again along with mixed liquid for iterative separation, so that the enrichment dehydration of the heavy non-aqueous phase pollution source and the deep purification of the aqueous phase are realized.
5. Effects of the implementation
The underground heavy non-aqueous phase liquid enrichment dehydration experiment is carried out by adopting tap water and trichloroethylene (5 percent, volume concentration) to simulate a place seriously polluted by DNAPLS, and the experiment temperature is 25 ℃. The physical parameters of trichloroethylene and water used are shown in Table 6 below and the results of the experiments are shown in Table 7 below.
TABLE 6 physical Property parameters
| Material(s) | Density/(kg/m) 3 ) | Kinematic viscosity/(kg/m.s) |
| Water (W) | 998.2 | 0.001003 |
| Trichloroethylene | 1446.89 | 0.00055 |
TABLE 7 Experimental results of underground heavy non-aqueous phase pollution source enrichment and dehydration
| Flow/(m) 3 /h) | Separation efficiency/%) | Water content of trichloroethylene/%) |
| 0.4 | 94.53 | 2.01 |
| 0.6 | 95.61 | 1.15 |
| 0.8 | 96.37 | 0.97 |
| 1.0 | 95.29 | 1.27 |
| 1.2 | 94.73 | 1.99 |
| 1.4 | 93.56 | 2.86 |
Note: trichloroethylene (TCE) is the DNAPLS organic pollutant with the highest detection rate in underground water monitoring of industrial pollution sites of many countries, and reaches up to 36.00 percent. Thus, the heavy non-aqueous phase liquid was replaced with TCE.
From the experimental results, the separation efficiency of the device on the mixed liquid is more than 93%, and the water content of the heavy non-aqueous phase liquid trichloroethylene after separation is less than 3%.
The above-listed embodiments are merely preferred embodiments of the present disclosure, and are not intended to limit the scope of the present disclosure. That is, all equivalent changes and modifications made according to the contents of the claims of the present application should be considered to be within the technical scope of the present disclosure.
All documents referred to in this disclosure are incorporated by reference into this application as if each were individually incorporated by reference. Furthermore, it should be understood that various changes or modifications to the disclosure may be made by those skilled in the art after reading the above teachings of the disclosure, and such equivalents may fall within the scope of the disclosure as defined by the appended claims.
Claims (10)
1. A self-overflowing iterative separation cyclone comprising: cylinder section (1), circular cone section (2), underflow pipe (3), interior overflow pipe (4), latus rectum overflow pipe (5), coalescence breakdown of emulsion bifidobacterium pipe import (6), interior overflow pipe outfall (7), latus rectum overflow pipe outfall (8), underflow opening (9) and overflow drainage venturi, wherein, overflow drainage venturi includes: a Venturi tube front section (10), a reducing section (11), a throat section (12), a gradually expanding section (13), a Venturi tube rear section (14) and a throat return pipe (15); the coalescence demulsification bifidotube inlet (6) is in horizontal tangential connection with the outer circumference of the upper end of the cylindrical section (1), the lower end of the cylindrical section (1) is connected with the upper end of the conical section (2), the lower end of the conical section (2) is connected with the upper end of the underflow pipe (3), the drift diameter overflow pipe (5) is positioned in the cylindrical section (1), the inner overflow pipe (4) is positioned in the drift diameter overflow pipe (5), the central axes of the drift diameter overflow pipe (5) and the inner overflow pipe (4) are coincided with the central axis of the cylindrical section (1), the lower end of the inner overflow pipe (4) is positioned between the upper part of the conical section (2) and the lower part of the drift diameter overflow pipe (5), the drift diameter overflow pipe (5) is vertical to the axis of the drift diameter overflow pipe outflow port (8), the drift diameter overflow pipe (5) is positioned above the cylindrical section (1), and the drift diameter overflow pipe outflow port (8) is connected with an overflow drainage throat backflow pipe (15), the inner overflow pipe (4) is coaxial with the inner overflow pipe outflow port (7), the inner overflow pipe outflow port (7) is positioned above the drift diameter overflow pipe (5), and the rear section (14) of the Venturi tube is connected with the coalescence demulsification bifidotube; the central axes of other parts of the overflow drainage Venturi tube except the throat return tube (15) are overlapped.
2. The self-overflowing iterative separation cyclone of claim 1, wherein the coalescence demulsifying bifido-tubing is internally filled with oleophilic and hydrophobic coalescence material, and branch tubing lengths thereof are equal.
3. The self-overflowing iterative separation cyclone of claim 1, wherein the bore overflow outlet (8) is connected with the outer circumference of the bore overflow (5) in a horizontal tangential direction.
4. The self-overflowing iterative separation cyclone according to claim 1, wherein the height of the cylindrical section (1) is 1.2-2 times the diameter of the cylindrical section (1), the diameter of the drift tube (5) is 0.6-0.8 times the diameter of the cylindrical section (1), the diameters of the internal overflow tube (4) and the underflow tube (3) are 0.2-0.5 times the diameter of the cylindrical section (1), and the cone angle of the conical section (2) is between 1.5-6 °.
5. The self-overflowing iterative separation cyclone of claim 1, wherein the inner overflow pipe (4) is inserted into the cylindrical section (1) to a depth of 0.4 to 0.9 times the diameter of the cylindrical section (1), and the drift diameter overflow pipe (5) is inserted into the cylindrical section (1) to a depth of 0.4 to 1.5 times the depth of the inner overflow pipe (4) into the cylindrical section (1).
6. The self-overflowing iterative separation cyclone according to claim 1, wherein the central axes of the cylindrical section (1), the conical section (2), the underflow pipe (3), the inner overflow pipe (4) and the drift diameter overflow pipe (5) of the cyclone are angled between 0-90 ° from the horizontal.
7. The self-overflow iterative separation cyclone according to claim 1, wherein the central axes of the venturi front section (10), the convergent section (11), the throat section (12), the divergent section (13) and the venturi rear section (14) in the overflow drainage venturi and the central axes of the cylindrical section (1), the conical section (2), the underflow pipe (3), the inner overflow pipe (4) and the drift diameter overflow pipe (5) in the cyclone are at an angle between 0 ° and 90 °.
8. Use of the self-overflowing iterative separation cyclone of any one of claims 1-7 for separation of DNAPLs in groundwater, wherein the cyclones are used singly or in parallel.
9. Use according to claim 8, wherein a plurality of cyclones are mounted in a pressure containing vessel, the central axes of the cyclones being parallel to the axis of the pressure containing vessel; a partition plate is arranged in the pressure-bearing tank body and used for fixing the cyclone and dividing the liquid phase storage volume; the pressure-bearing tank body is provided with a mixed liquid inlet, a light phase outlet and a heavy phase outlet.
10. Use according to claim 8 or 9, wherein the cyclone is mounted upside down in a pressure-containing tank.
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| CN201157703Y (en) * | 2007-11-28 | 2008-12-03 | 北京石油化工学院 | Compact type rotary flow air float separating device for oily wastewater treatment |
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