CN117366008B - Multiphase mixed transmission impeller with high light and heavy phase separation resistance - Google Patents
Multiphase mixed transmission impeller with high light and heavy phase separation resistance Download PDFInfo
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- CN117366008B CN117366008B CN202311428735.XA CN202311428735A CN117366008B CN 117366008 B CN117366008 B CN 117366008B CN 202311428735 A CN202311428735 A CN 202311428735A CN 117366008 B CN117366008 B CN 117366008B
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- 238000005191 phase separation Methods 0.000 title claims abstract description 18
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- 239000012071 phase Substances 0.000 abstract description 64
- 239000012530 fluid Substances 0.000 abstract description 35
- 239000007788 liquid Substances 0.000 abstract description 28
- 238000000926 separation method Methods 0.000 abstract description 22
- 239000007791 liquid phase Substances 0.000 abstract description 10
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- 230000000694 effects Effects 0.000 abstract description 4
- 230000016507 interphase Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 56
- 230000002776 aggregation Effects 0.000 description 23
- 230000002829 reductive effect Effects 0.000 description 20
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- 238000005054 agglomeration Methods 0.000 description 9
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D29/00—Details, component parts, or accessories
- F04D29/18—Rotors
- F04D29/181—Axial flow rotors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D3/00—Axial-flow pumps
- F04D3/02—Axial-flow pumps of screw type
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Abstract
The invention discloses a multiphase mixed delivery impeller with high light and heavy phase separation resistance, which relates to the field of mixed delivery pump fluid delivery, and comprises a multi-curvature gradual-increasing type hub and an inward-tilting type blade, wherein the gradual-increasing type hub adopts multi-curvature, namely three sections and more multi-curvature change rules are adopted in each part area of the hub, the front part small-curvature hub reduces the centrifugal force of the fluid by reducing the through-flow diameter of a flow channel, and the rear part large-curvature hub can reduce the radial velocity component, so that the aim of backward shifting the separation point of the light and heavy phase is fulfilled; the blade adopts an inward tilting type, and comprises an axial tilting angle alpha of the blade, and an included angle between a pressure surface and a back surface of the bladeThe internal inclined blade can provide extra centripetal force for fluid during operation, offset the displacement force between the gas phase and the liquid phase, further reduce the displacement degree of the inter-phase separation of the light phase and the heavy phase, and simultaneously combine the effect of the multi-curvature increasing type hub to delay the occurrence of the gas-liquid separation.
Description
Technical Field
The invention relates to a spiral axial flow type multiphase mixed transmission pump, in particular to a multiphase mixed transmission impeller with high light and heavy phase separation resistance.
Background
With the development of industrial level and scientific technology, the global demand for primary energy sources such as petroleum, natural gas and the like is increasing, the problem of resource degradation of land and shallow sea oil and gas is increasingly prominent, and the center of gravity of global oil and gas exploration and exploitation starts to shift to deep sea and open wells with high oil and gas discovery reserves.
The spiral axial flow type multiphase mixed transportation pump is used as key equipment of a multiphase mixed transportation system, has important significance for development of deep sea oil fields and oil fields in relatively remote areas, and compared with the traditional exploitation technology, the multiphase mixed transportation technology reduces complex separation equipment, a compressor, an oil transportation pump and two independent oil and gas transportation pipelines, and saves equipment cost and exploitation cost. The existing spiral axial flow type multiphase mixing and conveying pump is simple and compact in structure and suitable for conveying large-flow fluid media. However, in the process of mixing and conveying with high gas content, due to certain difference of density of light and heavy phase (gas phase and liquid phase) media, centrifugal forces born by the two phase media are different, and the two phase media are expressed as a certain displacement effect generated by the liquid phase and the gas phase media have radial motion components in the flowing direction; along the flowing direction, the pressure of the outlet of the impeller is far greater than the pressure of the inlet, the gas phase medium is subjected to a large reverse pressure gradient to be agglomerated at the outlet of the impeller, and cannot flow out of the impeller in time along with the main flow, so that the agglomeration of the gas phase is manifested as the reduction of the flow passage area, and the working performance of the mixing and conveying pump is directly influenced. With the development of petrochemical industry and the like, the spiral axial flow type gas-liquid mixing and conveying pump has higher requirements on the performance of the spiral axial flow type gas-liquid mixing and conveying pump under high gas content. The common spiral axial flow type gas-liquid mixing and conveying pump impeller can not meet the conveying requirement of high gas content gradually, and the problem of gas-liquid separation and gas phase aggregation in the mixing and conveying pump impeller become one of the main problems to be solved urgently in the multiphase mixing and conveying field at present.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides a multiphase mixed transmission impeller with high light and heavy phase separation resistance, which is mainly based on the hydrodynamic principle, and improves the radial components of gas phase generated by centrifugal force and the gas phase aggregation caused by reverse pressure gradient by changing the curvature structure of a hub and the inclination angle of a blade, so that the gas-liquid separation is finally delayed to the trailing edge of a blade grid, the gas phase aggregation degree is slowed down, and the transmission performance of a spiral axial flow type gas-liquid mixed transmission pump under high gas content is finally improved.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
a multiphase mixed-delivery impeller with high light and heavy phase separation resistance comprises a hub and blades,
the hub is a multi-curvature increasing hub, and is axially divided into three sections and more from frontThe curvature of the hub of each section after the hub is p 1 、ρ 2 、ρ 3 ……ρ n ，ρ 1 ＜ρ 2 ＜ρ 3 ……＜ρ n The whole hub has an increasing trend;
the blades are inwards inclined blades.
Further, the multi-curvature increasing hub is a triple-curvature increasing hub.
Further, for a three curvature increasing hub, the hub curvature ρ of the front portion 1 Hub curvature ρ of the intermediate portion 2 Hub curvature ρ of the rear part 3 Each hub curvature determination is performed according to a curvature determination scheme a or a curvature determination scheme B;
the curvature determination scheme a is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub;
on the basis, three equal division points are found at the axial distance, and two equal division points are respectively perpendicular to the axial direction and have the length d m1 Straight line M of (2) 1 And perpendicular to the axial direction and of length d m2 Straight line M of (2) 2 The method comprises the steps of carrying out a first treatment on the surface of the In straight line M 1 Taking up the tetrad point P 1 In straight line M 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Wherein d is h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle, take d m1 And/2 is a diameter drawing circle, taking the hub inlet and a straight line M 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle with radius, take a straight line M 2 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
The curvature determination scheme B is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub;
on the basis, four bisectors are found at the axial distance, and the length d is perpendicular to the axial direction through three four bisectors n1 Straight line N of (2) 1 And perpendicular to the axial direction and of length d n2 Straight line N of (2) 2 And perpendicular to the axial direction and of length d n3 Straight line N of (2) 3 ；
In straight line N 1 Taking up the tetrad point P 1 In straight line N 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Two sections, d h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle, take d n1 And/2 is a diameter drawing circle, taking the hub inlet and straight line N 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle for radius, take a straight line N 3 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
Based on the hub inlet diameter d h1 And hub outlet diameter d h2 The curvature determination scheme a or the curvature determination scheme B is selected, and is mainly determined according to the following conditions in order to ensure that the axial length H of the impeller is not changed:
a. if H/3 is less than or equal to d m1 4, processing according to a curvature determination scheme A;
b. if H/3 > d m1 And/4, processing according to a curvature determination scheme B.
Furthermore, the diameter change of the hub is gradually increased, smooth and excessive, so that the occurrence of convex points and concave points on the curve of the hub is avoided.
Further, the axial inclination angle of the inward-inclined blade is alpha, and the included angle between the pressure surface and the back surface of the blade is beta.
Further, the axial inclination angle α of the blade is obtained according to the following calculation formula:
wherein e is the distance between the wing-shaped rotation center and L is the distance between the hub and the rim at the middle of the impeller;
at the same time, it is also necessary to satisfy: the axial inclination direction of the blade is opposite to the flow direction; the e of several airfoils at the rim to the hub is gradually decreasing.
Further, the determination scheme of the included angle beta between the pressure surface and the back surface of the blade is as follows: beta is 0-6 deg.
Further, the included angle beta between the pressure surface and the back surface of the blade is 1-3 degrees.
The invention has the beneficial effects that:
(1) The blades adopt an inward-tilting design, and the spiral axial-flow type gas-liquid mixing pump rotates at a high speed along with the impeller in the process of conveying a two-phase medium, gas-liquid two-phase fluid moves from the impeller hub to the impeller rim under the action of centrifugal force, but the centrifugal force of the gas-liquid two-phase fluid is different due to different physical properties of the fluid, the fluid with large centrifugal force generates a squeezing force on the fluid with small centrifugal force, gas-phase fluid is gathered on the hub side under the action of squeezing force, and heavy-phase fluid is gathered on the rim side, so that a precondition is provided for later gas-phase gathering. The inward inclined blades can provide additional centripetal force for fluid, the centripetal force can offset the displacement force between the gas phase and the liquid phase to a certain extent, the displacement degree of the separation between the gas phase and the liquid phase is reduced, the radial velocity component of the gas phase in the flowing direction is finally reduced, and the gathering speed and the gathering degree of the gas phase on the hub side are reduced.
(2) The hub adopts a multi-curvature increasing hub design, firstly, compared with an original model impeller structure, the impeller structure with the variable hub curvature reduces the flow passage diameter of the impeller, the centrifugal force born by unit mass fluid in each area in the flow passage can be reduced, and then, the aggregation speed and aggregation degree of gas phase at the hub side are reduced by combining the action of the inward inclined blades; and secondly, in the process of conveying the two-phase medium, the impeller with the variable hub curvature can cause extra acceleration due to nonlinear change of the flow passage area, and the extra force generated by the extra acceleration acting on the fluid with unit mass flow can overcome the gas phase aggregation generated by the reverse pressure gradient to a certain extent, so that the gas phase at the hub side can flow out of the impeller as much as possible along with the main flow movement, and finally the gas-liquid separation is delayed, and the gas phase aggregation degree is reduced.
(3) According to the multiphase mixed transmission impeller with high light and heavy phase separation resistance, the extra centripetal force generated by the inward inclined blades resists the extrusion force generated by different physical properties between the light and heavy phases, the through-flow diameter of the impeller flow channel is reduced by combining the multi-curvature hub, the extrusion degree between the phases is reduced, the aggregation degree of the gas phase at the hub side is slowed down, and the occurrence of gas-liquid separation is delayed. In addition, the multi-curvature increasing hub can generate additional acceleration by changing the flow area, so that the fluid with unit mass flow obtains additional force for overcoming the reverse pressure gradient, and finally, the occurrence of gas-liquid separation is delayed, and the gas phase agglomeration degree is reduced. The invention can solve the problem of gas-liquid separation in the multiphase mixed transportation pump, avoid gas blockage, and provide a new thought and scheme for solving the problem of gas-liquid separation and gas phase aggregation in the multiphase mixed transportation pump.
Drawings
FIG. 1 is a schematic perspective view of an embodiment of the present invention;
FIG. 2 is a second perspective view of an embodiment of the present invention;
FIG. 3 is a side view of an embodiment of the present invention;
FIG. 4 is a schematic diagram of a three-curvature increasing hub in comparison with a conventional hub in accordance with an embodiment of the present invention;
FIG. 5 is a schematic illustration of a curvature determination scheme A for a three curvature incremental hub in an embodiment of the invention;
FIG. 6 is a schematic illustration of a curvature determination scheme B for a three curvature incremental hub in an embodiment of the invention;
FIG. 7 is a perspective view of an embodiment of an camber blade according to the present invention;
FIG. 8 is a second perspective view of an embodiment of an camber vane;
FIG. 9 is a perspective view of a camber blade according to an embodiment of the present invention;
FIG. 10 is a schematic view of the installation of an camber blade in an embodiment of the present invention;
FIG. 11 is a schematic top view of an embodiment of the present invention showing the angle of the tip-in vane.
The drawings are for illustrative purposes only and are not to be construed as limiting the present patent; for the purpose of better illustrating the embodiments, certain elements of the drawings may be omitted, enlarged or reduced and do not represent the actual product dimensions; it will be appreciated by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted.
Detailed description of the preferred embodiments
The present invention will be described in further detail with reference to specific examples, but is not limited thereto. In fig. 11, the left part of the picture is a blade airfoil at the rim seen from a top view, and the right part of the picture is a blade airfoil at the hub seen from a top view.
As shown in fig. 1 to 11, the present embodiment discloses a multiphase mixing impeller with high light and heavy phase separation resistance, which comprises a hub and blades.
The hub is a multi-curvature gradually-increased hub 1, the hub is axially divided into three sections and more, and the curvatures of the hub sections from front to back are ρ in sequence 1 、ρ 2 、ρ 3 ……ρ n ，ρ 1 ＜ρ 2 ＜ρ 3 ……＜ρ n The whole hub has an increasing trend.
Generally, multiple curvature incremental wheelsThe hub is a three-curvature increasing hub. As shown in fig. 4, the hub curvature ρ of the front part of the hub is three curvature increasing hub 1 Minimum, hub curvature ρ of the intermediate portion 2 Next, the hub curvature ρ of the rear portion 3 The maximum, wheel hub wholly is the trend of increasing, through the mode of reducing the wheel hub camber of anterior part and increase rear portion, reduce the centrifugal force that the unit mass flow fluid of relevant partial fluid produced, increase the excessive flow area of the rear portion that easily takes place the gas phase agglomeration and produce the extra power that is used for overcoming the gas phase agglomeration that the contrary pressure gradient leads to, combine the effect of infolding blade again, can delay the position of occurrence of gas-liquid separation, alleviate the gas phase agglomeration degree, make it take place to the cascade trailing edge part as far as possible, can promote the pumping performance that the mixing pump brought to a certain extent.
For a three curvature increasing hub, the hub curvature ρ of the front portion 1 Hub curvature ρ of the intermediate portion 2 Hub curvature ρ of the rear part 3 Each hub curvature determination is performed according to a curvature determination scheme a or a curvature determination scheme B;
as shown in fig. 5, the curvature determination scheme a is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub; this step is a routine technical capability for a person skilled in the art.
On the basis, three equal division points are found at the axial distance, and two equal division points are respectively perpendicular to the axial direction and have the length d m1 Straight line M of (2) 1 And perpendicular to the axial direction and of length d m2 Straight line M of (2) 2 The method comprises the steps of carrying out a first treatment on the surface of the In straight line M 1 Taking up the tetrad point P 1 In straight line M 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Wherein d is h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle, take d m1 And/2 is a diameter drawing circle, taking the hub inlet and a straight line M 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle with radius, take a straight line M 2 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
As shown in fig. 6, the curvature determination scheme B is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub;
on the basis, four bisectors are found at the axial distance, and the length d is perpendicular to the axial direction through three four bisectors n1 Straight line N of (2) 1 And a straight line N2 perpendicular to the axial direction and having a length dn2 and a straight line D perpendicular to the axial direction and having a length d n3 Straight line N of (2) 3 ；
In straight line N 1 Taking up the tetrad point P 1 In straight line N 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Two sections, d h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle, take d n1 And/2 is a diameter drawing circle, taking the hub inlet and straight line N 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle for radius, take a straight line N 3 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
Based on the hub inlet diameter d h1 And hub outlet diameter d h2 The curvature determination scheme a or the curvature determination scheme B is selected, and is mainly determined according to the following conditions in order to ensure that the axial length H of the impeller is not changed:
a. if H/3 is less than or equal to d m1 4, processing according to a curvature determination scheme A;
b. if H/3 > d m1 And/4, processing according to a curvature determination scheme B.
In the embodiment, the hub adopts a three-curvature increasing hub design, firstly, compared with an original model impeller structure, the impeller structure with the variable hub curvature reduces the flow passage diameter of the impeller, the centrifugal force born by fluid in each area in the flow passage is reduced, and then, the collection speed and the collection degree of gas phase at the hub side are reduced by combining the action of the inward inclined blades; secondly, in the process of conveying two-phase media, the impeller with the variable hub curvature causes extra acceleration due to nonlinear change of the flow passage area, and the extra force generated by the extra acceleration acting on the fluid with unit mass flow can overcome the gas phase aggregation generated by the reverse pressure gradient to a certain extent, so that the gas phase at the hub side can flow out of the impeller as much as possible along with the main flow movement, the gas-liquid separation is delayed finally, and the gas phase aggregation degree is reduced
As shown in fig. 1 to 11, the blade is an inward-inclined blade 2, and the inward-inclined blade 2 adopts a novel inward-inclined mode, wherein the axial direction of the blade has a certain inclination angle alpha, and the included angle between the pressure surface and the back surface of the blade is beta.
The axial inclination angle α of the inner inclined vane 2 is mainly affected by the curvature of the hub, and it is required to ensure that the flow passage presents a decreasing trend along the axial direction, so that acceleration occurs in the axial direction, and meanwhile, additional centripetal force can be generated in the radial direction to counteract the interphase force between the gas phase and the liquid phase. The included angle beta between the pressure surface and the back surface of the blade, the wrap angle and the initial position are mainly determined in the hydraulic design process according to the flow, the overflow area, the supercharging capacity and the comprehensive factors of the gas-liquid separation degree of the pump. On one hand, centripetal force generated by the inward-inclined blades in the operation process can resist the displacement force of light and heavy phases, reduce the displacement degree between gas and liquid phases, reduce the radial velocity component of gas phase, delay the occurrence process of gas-liquid separation, finally enable the gas-liquid separation to finally occur at the tail edge part of the blade grid, and reduce the gas phase aggregation degree.
The determination scheme of the axial inclination angle alpha of the blade and the included angle beta between the pressure surface and the back surface of the blade is as follows:
(1) The blade axial inclination angle α is obtained according to the following calculation formula:
as shown in fig. 6 and 7, e is the distance between the wing and the center of rotation, and L is the distance between the hub and the rim at the middle of the impeller.
At the same time, it is also necessary to satisfy: the axial inclination direction of the blades is opposite to the flow direction, so that the flowing fluid can be ensured to be acted by the blades, and centripetal force is generated. In the conventional axial-flow hydraulic machine design process, the e of the several airfoils from the rim to the hub is an increasing trend, and in the invention, in order to better meet the operation requirement and the performance requirement under the high air content, the trend is changed into gradually decreasing trend, so that the middle and rear parts of the blades can generate larger centripetal force on the fluid.
(2) The determination scheme of the included angle beta between the blade pressure surface and the back surface is as follows:
the included angle beta between the pressure surface and the back surface of the blade is generally 0-6 degrees as shown in fig. 10, but in the invention, the blade at the rim also needs to work on the fluid as much as possible, so that additional centripetal force is generated, and therefore, the angle should be 1-3 degrees under the condition of determining the thickness of the blade, so that the integral acting requirement of the blade is ensured.
In the embodiment, the blades are designed in an inward tilting mode, and the spiral axial-flow type gas-liquid mixing pump rotates at a high speed along with the impeller in the process of conveying the two-phase medium, gas-liquid two-phase fluid moves from the impeller hub to the impeller rim under the action of centrifugal force, but due to different physical properties of the fluid, the centrifugal force of the gas-liquid two-phase fluid is different, the fluid with large centrifugal force generates a squeezing force on the fluid with small centrifugal force, gas-phase fluid is gathered on the hub side under the action of squeezing force, and heavy-phase fluid is gathered on the rim side, so that a precondition is provided for later gas-phase gathering. The inward inclined blades can provide additional centripetal force for fluid, the centripetal force can offset the displacement force between the gas phase and the liquid phase to a certain extent, the displacement degree of the separation between the gas phase and the liquid phase is reduced, the radial velocity component of the gas phase in the flowing direction is finally reduced, and the gathering speed and the gathering degree of the gas phase on the hub side are reduced.
The working principle of the invention is as follows:
when the hub adopts multiple curvatures and fluid just enters the impeller, as shown in fig. 7, the through flow diameter of the fluid flow at the front part of the impeller is reduced in the small curvature hub part compared with that of the common hub, and the centrifugal force of the fluid in the unit mass flow of the part is also reduced in the small curvature hub part compared with that of the common hub, so that the occurrence of gas-liquid separation can be reduced; the multi-curvature increasing hub can enable the gas phase aggregation position to move backwards by changing the overflow area to enable the fluid with unit mass flow to generate additional force; under the action of the inward inclined blades, the blades provide additional centripetal force for the fluid, counteract the inter-phase extrusion force of the light gas phase and the liquid phase, and reduce the inter-phase separation extrusion degree; the adoption of the multi-curvature gradually-increased hub and the internal inclined blades reduces the centrifugal force of a gas-liquid separation part which is easy to occur and moves the gas phase agglomeration point backwards to a certain extent, and the external centripetal force is provided by the internal inclined blade, so that the final effect delays the occurrence position of the gas-liquid separation, the proportion of the gas phase agglomeration point in a flow channel is reduced, so that as much gas phase separation and gas phase agglomeration as possible occur at the tail edge part of the blade grid, and the high light-heavy phase separation and gas phase agglomeration resistance of the mixing pump is improved.
The invention can solve the problem of gas-liquid separation in the multiphase mixed transportation pump, avoid gas blockage, and provide a new thought and scheme for solving the problem of gas-liquid separation and gas phase aggregation in the multiphase mixed transportation pump.
The above embodiments are only for illustrating the technical solution of the present invention, and it should be understood by those skilled in the art that although the present invention has been described in detail with reference to the above embodiments: modifications and equivalents may be made thereto without departing from the spirit and scope of the invention, which is intended to be encompassed by the claims.
If the terms "first," "second," etc. are used herein to define a part, those skilled in the art will recognize that: the use of "first" and "second" is for convenience only as well as for simplicity of description, and nothing more than a particular meaning of the terms is intended to be used unless otherwise stated.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
Claims (6)
1. The utility model provides a high anti light heavy phase separation's heterogeneous mixed transportation impeller, includes wheel hub and blade, its characterized in that:
the hub is multi-curvedThe wheel hub with gradually increased rate is axially divided into three sections and more, and the curvatures of the wheel hubs of the sections from front to back are ρ 1 、ρ 2 、ρ 3 ……ρ n ，ρ 1 ＜ρ 2 ＜ρ 3 ……＜ρ n The whole hub has an increasing trend;
the blades are inwards inclined blades;
the multi-curvature increasing type hub is a three-curvature increasing type hub;
for a three curvature increasing hub, the hub curvature ρ of the front portion 1 Hub curvature ρ of the intermediate portion 2 Hub curvature ρ of the rear part 3 Each hub curvature determination is performed according to a curvature determination scheme a or a curvature determination scheme B;
the curvature determination scheme a is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub;
on the basis, three equal division points are found at the axial distance, and two equal division points are respectively perpendicular to the axial direction and have the length d m1 Straight line M of (2) 1 And perpendicular to the axial direction and of length d m2 Straight line M of (2) 2 The method comprises the steps of carrying out a first treatment on the surface of the In straight line M 1 Taking up the tetrad point P 1 In straight line M 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Wherein d is h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle, take d m1 And/2 is a diameter drawing circle, taking the hub inlet and a straight line M 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle with radius, take a straight line M 2 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
The curvature determination scheme B is performed as follows:
firstly, the inlet diameter d of a hub is designed according to the hydraulic design of a spiral axial-flow type oil-gas mixing and conveying pump h1 And an outlet diameter d h2 Performing preliminary calculation, and simultaneously combining the axial length H of the impeller obtained in the hydraulic calculation process to obtain basic parameters of a common hub;
on the basis, four bisectors are found at the axial distance, and the length d is perpendicular to the axial direction through three four bisectors n1 Straight line N of (2) 1 And perpendicular to the axial direction and of length d n2 Straight line N of (2) 2 And perpendicular to the axial direction and of length d n3 Straight line N of (2) 3 ；
In straight line N 1 Taking up the tetrad point P 1 In straight line N 2 Take up midpoint P 2 Connection P 1 And P 2 Extending to the diameter of the hub outlet, and the intersection point is P 3 ；P 3 Dividing the hub outlet diameter into d h2-1 And d h2-2 Two sections, d h2-1 Is a longer section;
the first section of the hub molded line is P 1 As the center of a circle by dn 1 And/2 is a diameter drawing circle, taking the hub inlet and straight line N 1 Is the hub curvature ρ 1 ；
The third section of the hub is P 3 As the center of a circle, take d h2-1 To draw a circle for radius, take a straight line N 3 And the middle part of the hub outlet is the hub curvature rho 3 ；
The second section is a middle part, and the hub curvature rho of the middle part is obtained by tangent of the first section and the third section 2 ；
Based on the hub inlet diameter d h1 And hub outlet diameter d h2 The curvature determination scheme a or the curvature determination scheme B is selected, and is mainly determined according to the following conditions in order to ensure that the axial length H of the impeller is not changed:
a. if H/3 is less than or equal to dm1/4, processing according to a curvature determination scheme A;
b. if H/3 > dm1/4, then processing is according to curvature determination scheme B.
2. The high light-heavy phase separation resistant multiphase mixing impeller of claim 1, wherein: the hub diameter change is gradually increased and smooth and excessive, so that the occurrence of convex points and concave points on the curve on the hub is avoided.
3. The high light-heavy phase separation resistant multiphase mixing impeller of claim 1, wherein: the axial inclination angle of the inward-inclined blade is alpha, and the included angle between the pressure surface and the back surface of the blade is beta.
4. The high light-heavy phase separation resistant multiphase mixing impeller of claim 3, wherein: the axial inclination angle alpha of the blade is obtained according to the following calculation formula:
wherein e is the distance between the wing-shaped rotation center and L is the distance between the hub and the rim at the middle of the impeller;
at the same time, it is also necessary to satisfy: the axial inclination direction of the blade is opposite to the flow direction; the e of several airfoils at the rim to the hub is gradually decreasing.
5. The high light-heavy phase separation resistant multiphase mixing impeller of claim 3, wherein: the determination scheme of the included angle beta between the pressure surface and the back surface of the blade is as follows: beta is 0-6 deg.
6. The high light-heavy phase separation resistant multiphase mixing impeller of claim 5, wherein: the included angle beta between the pressure surface and the back surface of the blade is 1-3 degrees.
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