CN111763547A - Full-rotational-flow supersonic separation device - Google Patents

Full-rotational-flow supersonic separation device Download PDF

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Publication number
CN111763547A
CN111763547A CN202010548769.2A CN202010548769A CN111763547A CN 111763547 A CN111763547 A CN 111763547A CN 202010548769 A CN202010548769 A CN 202010548769A CN 111763547 A CN111763547 A CN 111763547A
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section
laval nozzle
rotational flow
cyclone
flow
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CN111763547B (en
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边江
曹学文
李钰璇
谢振强
郭丹
刘杨
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China University of Petroleum East China
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China University of Petroleum East China
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/14—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by rotating vanes, discs, drums or brushes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/24—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by centrifugal force
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/02—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct with heating or cooling, e.g. quenching, means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/34—Applying ultrasonic energy
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/56—Specific details of the apparatus for preparation or upgrading of a fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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Abstract

The invention discloses a full-cyclone supersonic separation device which comprises a shell and a central cyclone component. The shell comprises a direct current flow stabilizing section, a Laval nozzle reducing section, a Laval nozzle expanding section and the like. The central rotational flow part comprises a front central rotational flow part and a rear central rotational flow part; the front central rotational flow component is positioned in the direct current steady flow section and the Laval nozzle reducing section; the rear central rotational flow component is positioned in the expansion section of the Laval nozzle. When gas enters the direct current steady flow section and the Laval nozzle reducing section, the gas flow expands in a rotational flow state, and reaches an ultrasonic speed after reaching the Laval nozzle expanding section, the temperature and the pressure are further reduced, the gas begins to condense, and the influence of liquid drop re-evaporation can be effectively reduced in the process of condensing while rotating flow; in addition, a cyclone component is also arranged in the Laval nozzle expansion section, the cyclone capacity is strong and durable, and the separation effect and the separation efficiency of the device are ensured.

Description

Full-rotational-flow supersonic separation device
Technical Field
The invention belongs to the technical field of low-temperature condensation and cyclone separation, and particularly relates to a full-cyclone supersonic separation device which is particularly suitable for low-temperature condensation and cyclone separation of impurity components such as water vapor, acid gas and heavy hydrocarbon of natural gas.
Background
In the field of natural gas exploitation, natural gas which is exploited at present is often saturated by water vapor and contains some heavy hydrocarbon components, and in order to meet the requirements of natural gas transportation and use, the water vapor, acid gas and the heavy hydrocarbon components must be separated.
Conventional natural gas separation processes include cooling, chemical absorption, adsorption, and membrane separation. However, these separation processes all have various disadvantages in the natural gas separation process, and there is a need to provide a new natural gas separation method.
The supersonic cyclone separation technology is a great innovation in the field of natural gas processing.
The supersonic cyclone separation technology combines the gas dynamics, engineering thermodynamics and hydromechanics theories, and the processing processes of expansion and temperature reduction, cyclone gas/liquid separation, recompression and the like are completed in a closed and compact device.
The separation technology has the advantages of simplicity, reliability, tightness, no leakage, no need of medicament, support of unattended operation and the like.
According to the installation position division of the cyclone component, the traditional supersonic cyclone separation device is mainly divided into the following two types:
the first is to install the cyclone part on the supersonic section behind the nozzle to generate cyclone, and the supersonic cyclone separation device with the structure has the following technical problems when natural gas separation is carried out:
because the speed conversion occurs under the supersonic speed condition, when the airflow meets the rotational flow component, shock waves are easily generated due to sudden change of the flow area, the low-temperature and low-pressure environment is damaged, secondary evaporation of condensed liquid drops is caused, and the separation efficiency of the device is reduced;
secondly, a rotational flow component is arranged at the inlet of the spray pipe, so that the gas enters the spray pipe in a rotational flow mode to be expanded and cooled, although the structure can effectively avoid the secondary evaporation of liquid drops, the following technical problems exist in the practical use:
due to the influence of the internal friction resistance of the supersonic separation device, the rotational flow speed of the supersonic separation device is obviously reduced along with the flowing of the gas, the separation effect of the supersonic separation device is reduced, and the condensed liquid drops are discharged along with the dry gas instead of being separated.
In addition, the shells of the two supersonic cyclone separation devices are integrally processed. When the integrally processed supersonic cyclone separation device is actually used, the following defects exist:
(1) the processing is difficult; (2) the contraction section and the diffusion section of the supersonic cyclone separation device are fixedly connected, so that free matching of the contraction section and the diffusion section of different types cannot be realized, and the adaptive working condition range of the device is narrow.
Disclosure of Invention
The invention aims to provide a full-cyclone supersonic separation device, so that the low-temperature condensation and cyclone separation effects of impurity components such as water vapor, acid gas and heavy hydrocarbon of natural gas can be effectively improved, and the separation efficiency of the device can be improved.
In order to achieve the purpose, the invention adopts the following technical scheme:
a full-cyclone supersonic separation device comprises a shell and a central cyclone component;
the shell comprises a steady flow contraction section and a diffusion separation section which are sequentially connected from front to back;
the steady flow contraction section comprises a straight pipe steady flow section and a Laval nozzle reducing section;
the straight pipe steady flow section is positioned at the front side of the Laval nozzle reducing section and is connected with the Laval nozzle reducing section;
the straight pipe steady flow section adopts a columnar structure; the Laval nozzle reducing section adopts a Vitosynes curve structure, namely the Laval nozzle reducing section gradually shrinks towards the diffusion separation section according to the Vitosynes curve by taking the joint of the Laval nozzle reducing section and the straight pipe steady flow section as a starting point;
the diffusion separation section comprises a Laval nozzle expansion section, an annular liquid collecting tank and a secondary diffusion section;
the Laval nozzle expansion section is connected with the Laval nozzle reducing section;
the Laval nozzle expansion section adopts a conical structure, namely the expansion trend is gradually formed from front to back;
the annular liquid collecting tank and the secondary diffusion section are nested into a whole, and the annular liquid collecting tank is positioned on the outer side of the secondary diffusion section;
the annular liquid collecting tank is coaxially connected with the secondary diffusion section;
the integral body consisting of the annular liquid collecting tank and the secondary diffusion section is positioned at the rear side of the Laval nozzle expansion section, and the Laval nozzle expansion section is connected with the integral body consisting of the annular liquid collecting tank and the secondary diffusion section;
the straight pipe flow stabilizing section, the Laval nozzle reducing section, the Laval nozzle expanding section and the annular liquid collecting tank are coaxially connected;
the central rotational flow part comprises a front central rotational flow part and a rear central rotational flow part; the front central rotational flow component is positioned in the straight pipe flow stabilizing section and the Laval nozzle reducing section, and the rear central rotational flow component is positioned in the Laval nozzle expanding section;
the front central rotational flow component comprises a front rotational flow blade support body and a plurality of front rotational flow blades;
the front part of the front end rotational flow blade support body is positioned in the straight pipe steady flow section and is in a semi-ellipsoid shape; the rear part of the front end swirl vane support body is positioned in the Laval nozzle reducing section and has a shape matched with the Laval nozzle reducing section;
each front-end swirl vane is respectively arranged on the front surface of the front-end swirl vane supporting body; the outermost side of the front-end swirl blade is in contact with the inner surface of the straight pipe flow stabilizing section, and the outermost side of the front-end swirl blade is clamped on the inner surface of the straight pipe flow stabilizing section;
the rear central rotational flow component comprises a rear rotational flow blade support body and a plurality of rear rotational flow blades;
the rear end rotational flow blade supporting body is connected with the front end rotational flow blade supporting body;
the length of the rear end rotational flow blade support body is equal to that of the Laval nozzle expansion section;
each rear-end swirl vane is installed along the length direction of rear-end swirl vane supporter in proper order, and along the length direction of rear-end swirl vane supporter, each rear-end swirl vane's size increases by preceding back in proper order.
Preferably, the rear end of the steady flow contraction section is connected with the front end of the diffusion separation section through a flange.
Preferably, the cross-sectional radius of the outlet at the rear end of the converging section of the Laval nozzle is the same as the cross-sectional radius of the inlet at the front end of the diverging section of the Laval nozzle.
Preferably, the annular sump comprises an annular sump outer side wall and an annular sump inner side wall; the front end of the outer side wall of the annular liquid collecting groove is connected with the rear end of the Laval nozzle expansion section; the front end of the inner side wall of the annular liquid collecting groove is connected with the front end of the secondary diffusion section.
Preferably, the secondary diffusion section is in a shape of a circular truncated cone, and the opening angle of the secondary diffusion section is the same as that of the Laval nozzle expansion section.
Preferably, the curve of the converging section of the Laval nozzle satisfies the following equation:
Figure BDA0002541691980000031
wherein x represents the axial distance from the front to the back at the inlet of the convergent section of the Laval nozzle;
wherein x at the inlet of the convergent section of the Laval nozzle is 0;
r represents the cross-sectional radius at axial distance x of the Laval nozzle tapered section;
l is the length of the convergent section of the Laval nozzle;
r1the radius of the cross section of the inlet of the convergent section of the Laval nozzle; r iscrIs the section radius of the outlet at the rear end of the tapered section of the Laval nozzle.
Preferably, the length of the Laval nozzle flare satisfies the following equation:
Figure BDA0002541691980000032
in the formula (I), the compound is shown in the specification,
Figure BDA0002541691980000033
the opening angle of the expansion section of the Laval nozzle;
r2the cross section radius of the outlet of the expansion section of the Laval nozzle is shown; l2Is the length of the Laval nozzle expansion segment.
The invention has the following advantages:
as mentioned above, the present invention is directed to a full-cyclone supersonic separation apparatus comprising a housing and a central cyclone member. The outer shell comprises a direct current flow stabilizing section, a Laval nozzle reducing section, a Laval nozzle expanding section and the like. The central rotational flow part comprises a front central rotational flow part and a rear central rotational flow part; wherein, the front central rotational flow component is positioned in the direct current steady flow section and the Laval nozzle reducing section; the rear central rotational flow component is positioned in the expansion section of the Laval nozzle. When gas enters the direct current steady flow section and the Laval nozzle reducing section, the gas flow expands in a rotational flow state, and reaches an ultrasonic speed after reaching the Laval nozzle expanding section 5, the temperature and the pressure are further reduced, the gas begins to condense, and the influence of liquid drop re-evaporation can be effectively reduced in the process of condensation while rotating flow; and a swirl component is also arranged in the Laval nozzle expansion section, so that the swirl capability is strong and durable, and the separation effect and the separation efficiency of the device are ensured. The invention effectively improves the low-temperature condensation and cyclone separation effect of impurity components such as water vapor, acid gas, heavy hydrocarbon and the like of the natural gas. In addition, the steady flow contraction section, the diffusion separation section and the central cyclone component are respectively processed and assembled and connected, so that the processing is easy, the assembly is convenient, and the adaptability of the full-cyclone supersonic separation device to different field working conditions is enhanced.
Drawings
Fig. 1 is a schematic structural diagram of a full-cyclone supersonic separation device in an embodiment of the invention.
Fig. 2 is a schematic structural diagram of a housing of the full-cyclone supersonic separation device in the embodiment of the invention.
FIG. 3 is an internal cross-sectional view of a full-cyclone supersonic separation apparatus in an embodiment of the present invention.
FIG. 4 is a schematic structural diagram of a central cyclone component of the full cyclone supersonic separation device in the embodiment of the invention.
Wherein, 1-steady flow contraction section, 2-diffusion separation section, 3-direct current steady flow section, 4-Laval nozzle reducing section, 5-Laval nozzle expanding section, 6-annular liquid collecting tank, 7-secondary diffusion section, 8-flange and 9-outermost point of front end swirl vane;
10-annular liquid collecting groove outer side wall, 11-annular liquid collecting groove inner side wall, 12-front central cyclone component, 13-rear central cyclone component, 14-front end cyclone blade supporting body, 15-front end cyclone blade, 16-rear end cyclone blade supporting body and 17-rear end cyclone blade.
Detailed Description
The invention is described in further detail below with reference to the following figures and detailed description:
as shown in FIG. 1, a full-cyclone supersonic separator comprises a shell, a central cyclone component and the like. Wherein, the shell comprises a steady flow contraction section 1 and a diffusion separation section 2 which are connected in sequence, as shown in fig. 2.
The left end in fig. 1 is defined as the front end of the separation device, and the steady flow contraction section 1 is located at the front side of the diffusion separation section 2.
The central cyclone component is positioned in the shell, namely in the steady flow contraction section 1 and the diffusion separation section 2.
The steady flow contraction section 1 comprises a straight pipe steady flow section 3 and a Laval nozzle reducing section 4.
The straight pipe flow stabilizing section 3 is positioned at the front side of the Laval nozzle reducing section and is connected with the Laval nozzle reducing section 4.
The straight tube steady flow section 3 adopts a columnar structure, as shown in figure 1.
The Laval nozzle reducing section 4 adopts a Vitosius curve structure, namely the Laval nozzle reducing section 4 gradually reduces towards the diffusion separation section 2 (from front to back) according to the Vitosius curve by taking the joint of the Laval nozzle reducing section and the straight pipe flow stabilizing section 3 as a starting point.
Through the structural design of the Laval nozzle reducing section 4, a uniform flow field is convenient to obtain.
The curve for the Laval nozzle tapered section 4 satisfies the following equation:
Figure BDA0002541691980000041
wherein x represents the axial distance from the front to the back at the inlet of the convergent section of the Laval nozzle;
wherein x at the inlet of the convergent section of the Laval nozzle is 0;
r represents the cross-sectional radius at axial distance x of the Laval nozzle tapered section; l is the length of the convergent section of the Laval nozzle;
r1the radius of the cross section of the inlet of the convergent section of the Laval nozzle; r iscrIs the section radius of the outlet at the rear end of the tapered section of the Laval nozzle.
As shown in fig. 2, the diffuser separation section 2 comprises a Laval nozzle expansion section 5, an annular sump 6 and a secondary diffuser section 7.
The Laval nozzle diverging section 5 is connected to the Laval nozzle tapering section 4.
The rear end outlet of the Laval nozzle tapered section 4 has the same section radius as the front end inlet of the Laval nozzle expanding section 5.
For convenience of processing and assembly, the rear end of the steady flow contraction section 1 (namely the rear end outlet of the Laval nozzle reducing section 4) is connected with the front end of the diffusion separation section 2 (namely the front end inlet of the Laval nozzle expanding section 5) by a flange 8.
The three parts of the steady flow contraction section 1, the diffusion separation section 2 and the central cyclone component can be respectively processed, assembled and used, so that the free matching of the steady flow contraction section 1, the diffusion separation section 2 and the central cyclone component in different models can be realized.
In addition, the self-regulation of refrigeration, rotational flow and diffusion can be realized simultaneously by the assembly type combination mode.
The following principle analysis is carried out on the technical effects brought by the assembled combination mode structure:
refrigeration
The steady flow contraction section 1 and the diffusion separation section 2 can jointly realize the refrigeration function;
when changing their radius, length, etc., the corresponding refrigeration performance, i.e., the temperature drop that the gas can achieve, differs in that the larger the radius, the shorter the length, the steeper the profile, i.e., the more rapid the contraction and expansion, and the faster the gas temperature drop.
② whirl
Different screw pitches correspond to different rotational flow strengths, and the larger the rotational flow strength is, the more thorough the liquid drop separation can be realized.
Diffusion
The function of the diffuser is mainly to recover a part of the pressure as a power source for the gas transport in the pipeline downstream of the separation device.
For example: impurities contained in the gas that are normally treated include water vapor, acid gases, and heavy hydrocarbons, but the natural gas produced from the off-gas field varies widely in composition, while in practice the acid gases are at a much lower temperature than is required for condensation of the water vapor.
If the acid gas content of the gas to be treated is high, a spray pipe with strong refrigerating performance needs to be selected;
if the radius of the condensed liquid drops is not large enough, a central cyclone component with high cyclone strength is needed, so that the central cyclone component can provide larger centrifugal separation capacity;
if the pressure required downstream of the separation device is high, a diffuser section with a large pressure recovery capacity is required.
Therefore, according to the different requirements, the three of the steady flow contraction section 1, the diffusion separation section 2 and the central rotational flow component need to be selected, and the assembly structure in the embodiment can realize free matching of the three in different models.
For the Laval nozzle divergent section 5, in order to simplify the design process and simultaneously realize expansion and rectification, the shape of the Laval nozzle divergent section is tapered by adopting a straight line method, that is, the Laval nozzle divergent section gradually expands from front to back.
The length of the Laval nozzle flare 5 satisfies the following equation:
Figure BDA0002541691980000051
in the formula (I), the compound is shown in the specification,
Figure BDA0002541691980000052
the opening angle of the expansion section of the Laval nozzle;
r2is represented by LaThe cross-sectional radius of the exit of the expansion section of the val nozzle; l2Is the length of the Laval nozzle expansion segment.
Laval nozzle principle: after the gas enters the Laval nozzle reducing section 4, the flow velocity is continuously increased (always at subsonic velocity), the temperature and the pressure are reduced, and the sound velocity is reached at the outlet of the Laval nozzle reducing section 4;
after the gas enters the Laval nozzle expansion section 5, the supersonic velocity is achieved, the temperature and the pressure are further reduced, and the gas begins to be condensed.
The annular liquid collecting groove 6 and the secondary diffusion section 7 are nested into a whole, the annular liquid collecting groove 6 is located on the outer side of the secondary diffusion section 7, and as shown in fig. 2, the annular liquid collecting groove 6 and the secondary diffusion section 7 are coaxially connected.
The whole composed of the annular liquid collecting groove 6 and the secondary diffusion section 7 is positioned at the rear side of the Laval nozzle expansion section 5, and the Laval nozzle expansion section 5 is connected with the whole composed of the annular liquid collecting groove 6 and the secondary diffusion section 7.
In particular, the annular sump 6 comprises an annular sump outer side wall 10 and an annular sump inner side wall 11, as shown in figure 3. Wherein, the front end of the outer side wall 10 of the annular liquid collecting groove is connected with the rear end of the Laval nozzle expansion section 5.
The front end of the inner side wall 11 of the annular liquid collecting groove is connected with the front end of the secondary diffusion section 7.
Through the structural design, the connection of the annular liquid collecting tank 6, the secondary diffusion section 7 and the Laval nozzle expansion section 5 is realized.
The annular liquid collecting tank 6 is used for collecting liquid drops separated from the gas-liquid mixture.
The straight pipe flow stabilizing section 3, the Laval nozzle reducing section 4, the Laval nozzle expanding section 5 and the annular liquid collecting tank 6 are coaxially connected.
As shown in fig. 4, the center cyclone part includes a front center cyclone part 12 and a rear center cyclone part 13.
Wherein the front central rotational flow component 12 is located in the straight tube flow stabilizing section 3 and the Laval nozzle tapered section 4, and the rear central rotational flow component 13 is located in the Laval nozzle expanding section 5, as shown in fig. 3.
The forward central swirl element 12 comprises a forward end swirl vane support 14 and a plurality of forward end swirl vanes 15.
As shown in FIG. 3, the front part of the front end swirl vane support 14 is located in the straight pipe flow stabilizing section 3 and is semi-ellipsoidal. The rear of the forward swirl vane support 14 is located within the Laval nozzle tapered section 4.
The rear of the forward swirl vane support 14 has a shape that conforms to the Laval nozzle tapered section 4.
Each of the front swirl vanes 15 is mounted on the front (i.e., semi-ellipsoidal) surface of the front swirl vane support body 14.
Taking one of the front swirl vanes 15 as an example: the outermost point 9 of the front end swirl vane is contacted with the inner surface of the straight pipe steady flow section 3, and the outermost point of the front end swirl vane 15 is clamped on the inner surface of the straight pipe steady flow section 3.
The inner and outer sides are relative to the front end swirl vanes, wherein the mounting side of the front end swirl vanes is the inner side.
The installation of the whole central rotational flow component is facilitated by clamping the front-end rotational flow blades 15 on the inner surface of the straight pipe flow stabilizing section 3.
The rear central swirl element 13 comprises a rear swirl vane support 16 and a plurality of rear swirl vanes 17.
The rear swirl blade support body 16 is connected to (the rear end of) the front swirl blade support body 14.
In the embodiment, the rear swirl blade support body 16 preferably adopts a straight rod structure, and the length of the rear swirl blade support body 16 is equal to that of the Laval nozzle expansion section 5.
Each rear-end swirl vane 17 is installed in order along the length direction of the rear-end swirl vane support body 16, and the size of each rear-end swirl vane 17 increases in order from front to back along the length direction of the rear-end swirl vane support body 16.
Because the continuous rotational flow blades are arranged in the separating device of the embodiment along the length direction of the separating device, a continuous, stable and lasting rotational flow field is formed in the straight pipe flow stabilizing section 3, the Laval nozzle reducing section 4 and the Laval nozzle expanding section 5, so that the condensed liquid drops are better separated from the main flow gas under the action of rotational flow, and the separating effect is improved.
Through the rear end whirl blade 17 that sets up not equidimension and pitch, can obtain different whirl intensity, specifically embody:
the size of the blade, i.e. the size of the blade (the height of a single blade in the direction perpendicular to the axial direction in fig. 4), is larger, i.e. the height above the axial direction of the rear central swirling member 13 is higher, the swirling ability is stronger;
the blade pitch is the distance between two adjacent blades (i.e. the distance between two adjacent blades in the axial direction in fig. 4), and the smaller the pitch between two adjacent blades is, i.e. the more twisted the blade swirl is, the stronger the swirl field obtained by the gas is.
The secondary diffusion section 7 is in a circular truncated cone shape, and the opening angle of the secondary diffusion section 7 is the same as that of the Laval nozzle expansion section 5. The secondary diffuser section 7 has the function of enabling the separated dry gas to recover a part of pressure and then be discharged from the outlet.
The installation process of the separation device in this embodiment is as follows:
firstly, inserting a central rotational flow component from the front side of the steady flow contraction section 1 (namely, inserting from the left side in the figure 3), and then sleeving a diffusion separation section 2 on the central rotational flow component from back to front (namely, from right to left in the figure 3);
and finally, connecting the joint of the steady flow contraction section 1 and the diffusion separation section 2 by using a flange 8.
The three components are simple in structure and convenient to assemble, and free matching among different models of the three components can be achieved according to requirements.
The working principle of the full-cyclone supersonic separation device in the embodiment is as follows:
after entering a separation device, natural gas containing impurities firstly flows through a straight pipe steady flow section 3 and then enters a Laval nozzle reducing section 4 to generate high-speed flow, the pressure and the temperature are reduced, meanwhile, rotational flow is generated under the action of a front-end rotational flow blade 15, and then the natural gas enters a Laval nozzle expanding section 5 to reach supersonic velocity after being expanded to form an ultralow temperature environment, condensable components in the gas are condensed into liquid drops, and the influence of liquid drop re-evaporation is effectively reduced in the process of rotating flow and condensing; in addition, because the rear-end swirl vane 17 is also arranged in the Laval nozzle expansion section 5, the condensed liquid drops are thrown to the wall surface of the Laval nozzle expansion section 5 by strong centrifugal force due to the swirl action of the rear-end swirl vane 17 to form a liquid film and flow into the annular liquid collecting tank 6, and the dry gas is recovered to partial pressure through the secondary diffuser section 7 and then is discharged from the outlet of the separation device, so that the separation effect of the supersonic separation device is ensured. Through the steps, the purposes of natural gas dehydration, heavy hydrocarbon removal, acid gas removal and the like can be effectively realized.
In the embodiment, the front-end cyclone blades 15 and the rear-end cyclone blades 17 can ensure that gas forms cyclone after entering the separation device and always maintains certain cyclone strength, so that the cyclone separation effect and the separation efficiency are ensured; the concrete expression is as follows:
in the two traditional supersonic cyclone separation devices, the cyclone blades are mounted at the front end of the separation device or at the rear end of the separation device, so that the separation capability is not durable, and the cyclone strength of a certain section in the separation device can be maintained.
The full-cyclone separation device provided by the invention is provided with the cyclone blades in the whole separation device, and the cyclone capacity of the separation device is strong and durable through the combined use of the front-end cyclone blade 15 and the rear-end cyclone blade 17.
The strong cyclone capacity can ensure that the centrifugal force applied to liquid drops in the gas is larger, and the liquid drops are more easily thrown to the wall surface of the shell of the separation device (namely, the Laval nozzle expansion section 5) and collected, so that the separation effect and the separation efficiency of the device are effectively improved.
It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.

Claims (7)

1. A full-cyclone supersonic separation device is characterized by comprising a shell and a central cyclone component;
the shell comprises a steady flow contraction section and a diffusion separation section which are sequentially connected from front to back;
the steady flow contraction section comprises a straight pipe steady flow section and a Laval nozzle reducing section;
the straight pipe steady flow section is positioned at the front side of the converging section of the Laval nozzle and is connected with the converging section of the Laval nozzle;
the straight pipe steady flow section adopts a columnar structure; the Laval nozzle reducing section adopts a Vitosynes curve structure, namely the Laval nozzle reducing section gradually shrinks towards the diffusion separation section according to the Vitosynes curve by taking the joint of the Laval nozzle reducing section and the straight pipe steady flow section as a starting point;
the diffusion separation section comprises a Laval nozzle expansion section, an annular liquid collecting tank and a secondary diffusion section;
the Laval nozzle expansion section is connected with the Laval nozzle reducing section;
the Laval nozzle expansion section adopts a conical structure, namely the expansion trend is gradually formed from front to back;
the annular liquid collecting tank and the secondary diffusion section are nested into a whole, and the annular liquid collecting tank is positioned on the outer side of the secondary diffusion section;
the annular liquid collecting tank is coaxially connected with the secondary diffusion section;
the integral body consisting of the annular liquid collecting tank and the secondary diffusion section is positioned at the rear side of the Laval nozzle expansion section, and the Laval nozzle expansion section is connected with the integral body consisting of the annular liquid collecting tank and the secondary diffusion section;
the straight pipe flow stabilizing section, the Laval nozzle reducing section, the Laval nozzle expanding section and the annular liquid collecting tank are coaxially connected;
the central rotational flow part comprises a front central rotational flow part and a rear central rotational flow part; the front central rotational flow component is positioned in the straight pipe flow stabilizing section and the Laval nozzle reducing section, and the rear central rotational flow component is positioned in the Laval nozzle expanding section;
the front central rotational flow component comprises a front rotational flow blade support body and a plurality of front rotational flow blades;
the front part of the front end rotational flow blade support body is positioned in the straight pipe steady flow section and is in a semi-ellipsoid shape; the rear part of the front-end swirl vane support body is positioned in the Laval nozzle reducing section and has a shape matched with the Laval nozzle reducing section;
each front-end swirl vane is respectively arranged on the front surface of the front-end swirl vane supporting body; the outermost side of the front-end swirl blade is in contact with the inner surface of the straight pipe flow stabilizing section, and the outermost side of the front-end swirl blade is clamped on the inner surface of the straight pipe flow stabilizing section;
the rear central rotational flow component comprises a rear rotational flow blade support body and a plurality of rear rotational flow blades;
the rear end rotational flow blade supporting body is connected with the front end rotational flow blade supporting body;
the rear end rotational flow blade support body adopts a straight rod structure, and the length of the rear end rotational flow blade support body is equal to that of the Laval nozzle expansion section;
each rear-end swirl vane is sequentially installed along the length direction of the rear-end swirl vane support body, and the size of each rear-end swirl vane is sequentially increased from front to back along the length direction of the rear-end swirl vane support body.
2. Full-cyclone supersonic separation device according to claim 1,
the rear end of the steady flow contraction section is connected with the front end of the diffusion separation section through a flange.
3. Full-cyclone supersonic separation device according to claim 1,
the rear end outlet of the Laval nozzle reducing section and the front end inlet section radius of the Laval nozzle expanding section are the same.
4. Full-cyclone supersonic separation device according to claim 1,
the annular liquid collecting groove comprises an annular liquid collecting groove outer side wall and an annular liquid collecting groove inner side wall; the front end of the outer side wall of the annular liquid collecting groove is connected with the rear end of the Laval nozzle expansion section; the front end of the inner side wall of the annular liquid collecting groove is connected with the front end of the secondary diffusion section.
5. Full-cyclone supersonic separation device according to claim 1 or 4,
the secondary diffusion section is in a circular truncated cone shape, and the opening angle of the secondary diffusion section is the same as that of the Laval nozzle expansion section.
6. Full-cyclone supersonic separation device according to claim 1,
the curve of the convergent section of the Laval nozzle meets the following equation:
Figure FDA0002541691970000021
wherein x represents the axial distance from the front to the back calculated from the inlet of the convergent section of the Laval nozzle;
wherein x at the inlet of the convergent section of the Laval nozzle is 0;
r represents the cross-sectional radius at axial distance x of the Laval nozzle tapered section;
l is the length of the convergent section of the Laval nozzle;
r1the radius of the cross section of the inlet of the convergent section of the Laval nozzle; r iscrIs the section radius of the outlet at the rear end of the tapered section of the Laval nozzle.
7. Full-cyclone supersonic separation device according to claim 6,
the length of the Laval nozzle expansion section satisfies the following formula:
Figure FDA0002541691970000022
in the formula (I), the compound is shown in the specification,
Figure FDA0002541691970000023
the opening angle of the expansion section of the Laval nozzle;
r2the cross section radius of the outlet of the expansion section of the Laval nozzle is shown; l2Indicating the length of the Laval nozzle flare.
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