WO2022105699A1 - 一种自适应多相一体化分离装置和方法 - Google Patents

一种自适应多相一体化分离装置和方法 Download PDF

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WO2022105699A1
WO2022105699A1 PCT/CN2021/130520 CN2021130520W WO2022105699A1 WO 2022105699 A1 WO2022105699 A1 WO 2022105699A1 CN 2021130520 W CN2021130520 W CN 2021130520W WO 2022105699 A1 WO2022105699 A1 WO 2022105699A1
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Prior art keywords
separation
pipe
main
auxiliary
phase
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PCT/CN2021/130520
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English (en)
French (fr)
Inventor
杨强
刘懿谦
卢浩
潘志程
钱运东
李裕东
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华东理工大学
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Priority to EP21893846.2A priority Critical patent/EP4249101A1/en
Publication of WO2022105699A1 publication Critical patent/WO2022105699A1/zh

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    • 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
    • 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
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0217—Separation of non-miscible liquids by centrifugal force
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0042—Degasification of liquids modifying the liquid flow
    • B01D19/0052—Degasification of liquids modifying the liquid flow in rotating vessels, vessels containing movable parts or in which centrifugal movement is caused
    • B01D19/0057—Degasification of liquids modifying the liquid flow in rotating vessels, vessels containing movable parts or in which centrifugal movement is caused the centrifugal movement being caused by a vortex, e.g. using a cyclone, or by a tangential inlet
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2427—The feed or discharge opening located at a distant position from the side walls
    • 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
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/08—Vortex chamber constructions
    • B04C5/103—Bodies or members, e.g. bulkheads, guides, in the vortex chamber
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the invention belongs to the fields of petrochemical industry and environmental protection, and in particular relates to an adaptive multiphase integrated separation device and method.
  • Oily wastewater not only has a wide range of sources but also has complex components. Every year, 50 million to 100 million tons of oily substances enter water bodies in the world, causing great harm to the marine and river water environment and soil environment.
  • the current oily wastewater treatment technology usually only performs a single treatment for the oil content, but the actual oily wastewater, especially the oily wastewater from oil and gas exploration and petrochemical industries, usually contains a large amount of dissolved and undissolved gases and suspended solid particles, which can realize the turbidity of oil and gas. Collaborative separation is an important direction of current technological development.
  • CN201720744919.0 discloses a degassing and degreasing hydraulic coalescing device, the main purpose of which is to provide a novel separation device for gas-liquid-liquid three-phase medium separation.
  • the invention does not further describe its turbidity removal performance, and there is still a limitation that the processing capacity of the current hydrocyclone technology equipment is small.
  • CN201611062892.3 discloses a method for dust removal and degreasing of coal chemical wastewater with filtration and retention as the basic principle.
  • the invention takes into account the consideration of solid particle removal, but the equipment takes filtration and retention as the basic principle, which inevitably faces the problem of excessive floor space. Large, filter material or filter media backwash replacement and other issues.
  • the present invention provides an adaptive multiphase integrated separation device and method, so as to solve the problems of gas-phase impact, narrow operating elastic range, etc. series of questions.
  • an adaptive multi-phase integrated separation device the separation device includes more than one integrated separation core tube, and the integrated separation core tube includes The main separation pipe, the auxiliary separation pipe, and the main and auxiliary pipe communication pipes connecting the main separation pipe and the auxiliary separation pipe, and two or more of the auxiliary separation pipes are arranged around one of the main separation pipes;
  • the main separation pipe The bottom inlet of the pipe is provided with a swirling device, and the swirling flow field generated by the swirling device converts the liquid flowing through the main separation pipe from axial motion to rotational motion;
  • the tangential swirling opening of the auxiliary separation tube makes the liquid flowing through the auxiliary separation tube enter the auxiliary separation tube tangentially to make a rotary motion;
  • the bottom of the auxiliary separation tube is provided with a cone A cone-shaped or convex-shaped heavy-phase separation cone.
  • the present invention further provides that the number of the auxiliary separation pipes is 1-6, and the flow field rotation direction of the auxiliary separation pipe is clockwise or counterclockwise, which is the same or opposite to the flow field rotation direction of the main separation pipe.
  • the present invention further provides that the main separation tube is a main separation cavity, and the auxiliary separation tube is a secondary separation cavity; the upper part of the main separation tube is provided with a light-phase drainage cone of the main separation cavity, and the upper part of the auxiliary separation tube is provided with a light-phase drainage cone of the main separation cavity.
  • a secondary separation chamber is provided with a light-phase drainage cone.
  • the inclination angle of the light-phase drainage cone of the main separation chamber is 10° to 75°, and a main drainage channel with an included angle of 0° to 10° is opened in the middle of the light-phase drainage cone of the main separation chamber.
  • the diameter of the main drainage channel is 0.1-0.8 times the diameter of the main separation cavity; the inclination angle of the light-phase drainage cone of the auxiliary separation cavity is 10-75°, and the middle of the light-phase drainage cone of the auxiliary separation cavity is 10-75°.
  • a secondary drainage channel with an included angle of 0 to 10° is opened, and the diameter of the secondary drainage channel is 0.1 to 0.8 times the diameter of the secondary separation cavity.
  • the present invention further provides that the top of the main separation pipe is provided with a main separation cavity anti-flushing cap, and the top of the auxiliary separation pipe is provided with a secondary separation cavity anti-flushing cap.
  • the spin generator is a guide vane, and the helical inclination angle of the guide vane is 10° to 75°; or, the spin generator is a tangential inlet, and the number of the tangential inlets is 1 to 6.
  • the length of the main separation pipe is 1 to 20 times the inner diameter
  • the length of the auxiliary separation pipe is 1 to 20 times the inner diameter
  • the inclination angle of the heavy phase separation cone is 10-75°, and the diameter is 0.2-0.8 times the inner diameter of the auxiliary separation pipe.
  • the present invention further provides that a distribution pipe is connected to the bottom of each of the main separation pipes, a communication pipe is commonly connected to the sides of the distribution pipe, and a distribution pipe is commonly connected to the bottom of the distribution pipe.
  • the ends are commonly connected with a distribution tank, and the bottom of the distribution tank is connected with an inlet pipe.
  • the distribution pipes are evenly distributed radially and radially with the center of the distribution tank as the center of the circle, and the number is 2-6.
  • the present invention further provides that, if there are multiple integrated separation core tubes, the distribution method is to form a triangular shape, a radial shape or a combination of the two shapes with the distribution tank as the center, and the distribution circles are 1-6.
  • an adaptive multiphase integrated separation method comprises the following steps:
  • the material to be processed enters the main separation pipe
  • the present invention further provides that the size of the large bubbles is greater than 10 ⁇ m, the size of the large particle size oil droplets is greater than 20 ⁇ m, the size of the small bubbles is 5-10 ⁇ m, and the size of the small particle size oil droplets is 10-20 ⁇ m.
  • the acceleration of processing the main phase in the main separation tube is 5-5000 times the acceleration of gravity
  • the acceleration of processing the main phase in the auxiliary separation tube is 10-10,000 times the acceleration of gravity
  • an adaptive multiphase integrated separation method comprises the following steps:
  • the material to be processed enters the distribution tank through the inlet pipe, and after buffering in the distribution tank, the material to be processed enters the distribution pipe, the material reaches the distribution pipe through the distribution pipe, and the distribution pipes are connected by a communication pipe to ensure the uniform distribution of the material.
  • the tube enters the integrated separation core tube;
  • the material to be treated first enters the main separation pipe of the integrated separation core pipe, and through the action of the swirl field in the main separation pipe, the large air bubbles and oil droplets with large particle sizes are removed and adhered to the large air bubbles and oil droplets with large particle sizes. suspended solids;
  • the present invention further provides that the integrated separation core tube is single or multiple, and the pressure drop of the integrated separation core tube is less than or equal to 0.3 MPa.
  • the present invention has the following beneficial effects:
  • the present invention realizes the coordinated separation of oil, gas and turbidity through the coupling structure of the main separation pipe and the auxiliary separation pipe.
  • the oil phase removal rate and the gas phase removal rate of the present invention are both greater than 90%, and the processing capacity has extremely high operational flexibility. Compared with the traditional cyclone field separation method, the processing capacity has extremely high processing capacity Operation flexibility, 50%-150%, suitable for compact treatment of high oil and high turbidity sewage, high separation efficiency, achieves the purpose of compact and fast separation in short process, and can effectively reduce the floor space of relevant separation systems , make up for the shortcomings of the existing technology.
  • the pressure drop of the integrated separation core tube is less than or equal to 0.3Mpa.
  • Figure 1-1 is a schematic structural diagram of an adaptive multi-phase integrated separation device
  • Figure 1-2 is another structural schematic diagram of the self-adaptive multi-phase integrated separation device
  • Fig. 2 is the structural representation of the main separation pipe
  • Fig. 3 is the structural representation of the auxiliary separation pipe
  • Figure 4-1 to Figure 4-4 respectively show that the number of auxiliary separation pipes is 2 (the direction of rotation is the same as that of the main separation pipe), 2 (the direction of rotation is opposite to that of the main separation pipe), and 3 (the direction of rotation is the same as that of the main separation pipe)
  • Figure 5-1 is a schematic diagram of the structure of the guide vane
  • Figure 5-2 is a schematic structural diagram of a rotary guide vane
  • Figure 6-1 is a top view of the structure of a tangential inlet
  • Figure 6-2 is a top view of the structure of three tangential inlets
  • Figure 7-1 is a schematic diagram of the assembly of multiple integrated separation core tubes (multiple distribution tubes, only one integrated separation core tube is shown);
  • Figure 7-2 is a partial top view of the structure of Figure 7-1;
  • Figure 8-1 is a schematic diagram of the assembly of multiple integrated separation core tubes (for a single distribution tube, only one integrated separation core tube is shown);
  • Figure 8-2 is a partial top view of the structure of Figure 8-1;
  • Figures 9-1 to 9-3 show the layout of the integrated separation core tubes (respectively, triangular arrangement, radial arrangement, and triangular combined radial arrangement).
  • FIG. 10 is a schematic diagram of the installation structure in the vertical equipment of the present invention.
  • FIG. 11 is a schematic diagram of the installation structure in the horizontal equipment of the present invention.
  • 1-1 vortex generator
  • 1-2 main separation chamber
  • 1-3 main separation chamber light-phase drainage cone
  • 1-4 main separation chamber anti-wash cap
  • 1-5 guide vane
  • 1-6 Tangential inlet
  • 1-7 main drainage channel.
  • 2-1 Auxiliary separation tube tangential swirl
  • 2-2 Heavy phase separation cone
  • 2-3 Auxiliary separation cavity
  • 2-4 Auxiliary separation cavity light phase drainage cone
  • 2-5 Auxiliary separation cavity prevention Cap flushing
  • 2-6 auxiliary drainage channel.
  • 0-1 Integrated separation core tube
  • 0-2 Distribution tube
  • 0-3 Distribution tube
  • 0-4 Inlet tube
  • 0-5 Unicom tube
  • 0-6 Distribution tank.
  • the separation device includes more than one integrated separation core tube 0-1, and the integrated separation core tube 0-1 includes a main separation tube 1, a secondary separation tube 2 and a communication
  • the main separation pipe 1 and the auxiliary separation pipe 2 communicate with the main and auxiliary pipes 3 , and two or more auxiliary separation pipes 2 are arranged around one main separation pipe 1 .
  • the bottom inlet of the main separation pipe 1 is provided with a cyclone 1-1, and the cyclone field generated by the cyclone 1-1 converts the liquid flowing through the main separation pipe 1 from axial motion to rotational motion.
  • the auxiliary separation pipe 2 is provided with a tangential swirling port 2-1 of the auxiliary separation pipe along the axial direction. Rotational movement.
  • a conical or convex-shaped heavy phase separation cone 2-2 is arranged at the bottom of the secondary separation tube 2.
  • a connecting piece 4 can be connected at the bottom of the main separation pipe 1 for connecting to other equipment or pipes.
  • a connecting piece 4 can be connected at the bottom of the main separation pipe 1 for connecting to other equipment or pipes.
  • other pipes and the like can be connected through the connecting piece 4.
  • the main separation tube 1 is a main separation chamber 1-2
  • the auxiliary separation tube 2 is a secondary separation chamber 2-3.
  • the upper part of the main separation pipe 1 is provided with a main separation cavity light-phase drainage cone 1-3
  • the upper part of the auxiliary separation pipe 2 is provided with a secondary separation cavity light-phase drainage cone 2-4.
  • the number of the auxiliary separation pipes 2 is 1-6, and the flow field rotation direction of the auxiliary separation pipe 2 is clockwise or counterclockwise, which is the same or opposite to the flow field rotation direction of the main separation pipe 1 .
  • the structure in which the number of auxiliary separation tubes 2 is 2 or 3 can be seen in FIGS. 4-1 to 4-4.
  • the inclination angle of the light-phase drainage cone 1-3 of the main separation cavity is 10-75°, and the main separation-cavity light-phase drainage cone 1-3 is provided with main drainage channels 1-7 with an included angle of 0-10°.
  • the diameter of the main drainage channel 1-7 is 0.1 to 0.8 times the diameter of the main separation cavity 1-2.
  • the inclination angle of the light-phase drainage cone 2-4 of the auxiliary separation chamber is 10-75°, and the auxiliary drainage channel 2-6 with an included angle of 0-10° is arranged on the light-phase drainage cone 2-4 of the auxiliary separation chamber.
  • the diameter of the channel 2-6 is 0.1-0.8 times the diameter of the auxiliary separation chamber 1-2.
  • the top of the main separation pipe 1 is provided with a main separation cavity anti-flushing cap 1-4 for anti-flushing, and the top of the auxiliary separation pipe 2 is provided with a secondary separation cavity anti-flushing cap 2-5.
  • the spinner 1-1 is a guide vane 1-5, and the helix angle of the guide vane 1-5 is 10-75°.
  • the spin generator 1-1 is a tangential inlet 1-6, and the number of the tangential inlets 1-6 is 1-6.
  • the length of the main separation pipe 1 is 1 to 20 times the inner diameter
  • the length of the auxiliary separation pipe 2 is 1 to 20 times the inner diameter
  • the inclination angle of the heavy phase separation cone 2-2 is 10-75°, and the diameter is 0.2-0.8 times the inner diameter of the auxiliary separation pipe 2 .
  • the material separation process in this embodiment is as follows: the material to be treated enters the self-adaptive degassing, oil and turbidity integrated separation core tube 0-1 of the main and auxiliary chambers to realize the coordinated and integrated separation of oil, gas and turbidity; the material After the separation is completed, it is buffered by a vertical container, and the gas phase, the turbid oil-containing phase, and the treated water are discharged through the corresponding interface.
  • a distribution pipe 0-2 is connected to the bottom of each main separation pipe 1, and a communication pipe is commonly connected to the side of the distribution pipe 0-2 0-5, the bottom of the distribution pipe 0-2 is connected to the distribution pipe 0-3, and the end of the distribution pipe 0-3 is connected with the distribution tank 0-6.
  • the distribution tank 0-6 is a horizontal or vertical container.
  • An inlet pipe 0-4 is connected to the bottom of the tank 0-6.
  • the distribution pipes 0-3 are evenly distributed radially and radially with the center of the distribution tank 0-6 as the center of the circle, and the number is 2-6.
  • D is the inner diameter of the main separation pipe 1
  • d is the inner diameter of the sub-separation pipe 2 .
  • the integrated separation core tube 0-1 is set to be single or multiple according to the different design processing capacity of the equipment. If the size of the equipment is large enough, multiple tubes can be arranged. If there are multiple integrated separation core tubes 0-1, the distribution method is to form a triangle, a radial shape or a combination of the two shapes with the distribution tank 0-6 as the center, and the distribution circles are 1 to 6, see Figure 9- 1 to Figure 9-3.
  • the present invention may be installed in either vertical equipment or horizontal equipment.
  • the material separation process of this embodiment is as follows: the material to be processed enters the distribution tank 0-6 through the inlet pipe 0-4; after buffering in the distribution tank 0-6, the material to be processed enters the distribution pipe 0-3 uniformly distributed in the circumferential direction; The distribution pipe 0-3 reaches the distribution pipe 0-2, and the distribution pipes 0-2 are connected by the communication pipe 0-5 to ensure the uniform distribution of the material; the material enters the main and auxiliary cavity through the distribution pipe 0-2.
  • Oil removal and turbidity integrated separation core tube 0-1 realizes the coordinated and integrated separation of oil, gas and turbidity; after the separation of the material is completed, it is buffered by a vertical container, and the gas phase, the turbid oil phase, and the treated water are corresponding to each other through the corresponding interface. Efflux.
  • This embodiment provides a more specific structure of the self-adaptive integrated separation device.
  • a vertical tank is provided with a plurality of sets of separators combined with main and auxiliary chambers in parallel to achieve efficient and rapid separation.
  • the distribution tank 0-6 is a cylindrical container with an oval head, and the entire distribution tank 0-6 can be filled by running 0.3s at the maximum processing capacity.
  • the three distribution pipes 0-3 are centered on the center of the distribution tank 0-6. It is evenly distributed radially outward, and the included angle between each adjacent two distribution pipes 0-3 is 120°.
  • the inner diameter of the Unicom tube 0-5 is 0.8 times the inner diameter of the inlet tube 0-4, the inner diameter of the distribution tube 0-2 is consistent with the inner diameter of the main separation tube 1, and a total of 40 integrated separation core tubes 0-1 are used, and the distribution is mixed in a triangle. Radial distribution arrangement, the number of distribution circles is 3 circles.
  • the liquid flow velocity in the inlet pipe 0-4 size is 1.5m/s.
  • the connecting piece 4 is connected with a flange.
  • the rotation direction of the flow field in the main separation chamber 1-2 is clockwise.
  • the communication pipe 3 of the main and auxiliary pipes is tangentially connected to the main separation chamber 1-2 and the auxiliary separation chamber 2-3 with a rectangular section, and the cross-sectional area is 0.5 times the cross-sectional area of the auxiliary separation chamber 2-3.
  • the swirler 1-1 of the main separation pipe 1 uses guide vanes 1-5 with a clockwise direction of rotation, and the vane helical inclination angle ⁇ is 45°.
  • the angle ⁇ 2 is 20°.
  • the average water and oil content produced by the equipment imported is 2000mg/L, and the highest is 3000mg/L.
  • the dissolved gas is saturated at the equipment inlet, and the gas phase is about 10% by volume, and the turbidity concentration is about 1000mg/L.
  • the average value of the oil content in the water phase outlet is lower than 150mg/L, the minimum can be lower than 90mg/L, the gas phase removal rate after separation is >95%, and the overall pressure drop of the equipment is ⁇ 0.2MPa.

Abstract

一种自适应多相一体化分离装置和方法，分离装置包括一根以上一体化分离芯管(0-1)，一体化分离芯管(0-1)包括主分离管(1)、副分离管(2)以及连通主分离管(1)和副分离管(2)的主副管联通管(3)；主分离管(1)的底部进口设有造旋器(1-1)，副分离管(2)沿轴向设有副分离管切向造旋口(2-1)，副分离管(2)内的底部设有锥形或凸台形的重相分离锥(2-2)。该分离装置通过主分离管(1)与副分离管(2)的耦合结构实现对油、气、浊的协同分离，且对物料中油、气、浊含量的波动具备极高的适应性。与传统的旋流场分离方法相比，利用该分离装置进行分离其处理量具有操作弹性，适用于对高含油、高含浊污水的紧凑处理，分离效率较高，可实现短流程下紧凑、快速分离的目的，能够有效降低相关分离系统的占地面积。

Description

一种自适应多相一体化分离装置和方法 技术领域
本发明属于石油化工和环保领域，具体涉及一种自适应多相一体化分离装置和方法。
背景技术
在石油化工、煤化工、冶金、机械制造、纺织印染、制药、食品加工、餐饮等行业生产中会有大量含油废水产生，含油废水不仅来源广泛且成分复杂。世界上每年有5000万至10000万吨油类物质进入水体，对海洋和河流水体环境、土壤环境造成极大危害。当前含油废水处理技术通常仅针对油含量进行单一的处理，而实际的含油废水，尤其是油气开采、石油化工行业的含油废水中通常含有大量溶解及非溶解气体、悬浮固体颗粒，实现油气浊的协同分离是当前技术发展的一个重要方向。在当前的脱气除油设备中，如水力旋流器、管式分离器等利用旋流场进行分离的技术设备因其结构紧凑、无动部件而得到了广泛应用，但限制其发展的一个重大因素是其最佳操作流量范围窄，需要相对严格控制设备的处理量。
CN201720744919.0公开了一种脱气除油水力聚结装置，其主要目的在于提供一种用于气-液-液三相介质分离的新型分离装置。该发明并未对其除浊性能进行进一步描述，仍存在当前水力旋流技术设备处理量较小的局限。CN201611062892.3公开了一种过滤截留为基本原理的适用于煤化工废水除尘除油方法，该发明兼顾了对固体颗粒物脱除的考虑，但设备以过滤截留为基本原理，必然面临占地面积过大、滤料或过滤介质的反洗更换等问题。
为此，亟需一种可以实现油、气、浊协同去除分离的自适应性分离方法及相关装置。
发明内容
本发明针对现有技术存在的不足，提供一种自适应多相一体化分离装置和方法，以解决现有利用旋流场进行分离的技术设备所面临的受气相冲击、操作弹性范围窄等一系列问题。
为解决上述技术问题，本发明提供的第一个技术方案如下：一种自适应多相一体化分离装置，所述分离装置包括一根以上一体化分离芯管，所述一体化分离芯管包括主分离管、副分离管以及连通所述主分离管和所述副分离管的主副管联通管，一个所述主分离管的周围设有2个以上所述副分离管；所述主分离管的底部进口设有造旋器，所述造旋器产生的旋流场使流过所述主分离管的液体由轴向运动变换为旋转运动；所述副分离管的沿轴向设有副分离管切向造旋口，所述副分离管切向造旋口使流过所述副分离管的液体通过切向进入副分离管做旋转运动；所述副分离管内的底部设有锥形或凸台形的重相分离锥。
本发明进一步设置为，所述副分离管的数量为1～6，所述副分离管的流场旋向为顺时针或逆时针，与所述主分离管的流场旋向相同或相反。
本发明进一步设置为，所述主分离管内为主分离腔，所述副分离管内为副分离腔；所述主分离管的上部设有主分离腔轻相引流锥，所述副分离管的上部设有副分离腔轻相引流锥。
本发明进一步设置为，所述主分离腔轻相引流锥的倾斜夹角为10～75°，所述主分离腔轻相引流锥的中间开有夹角为0～10°的主引流孔道，所述主引流孔道的直径为所述主分离腔直径的0.1～0.8倍；所述副分离腔轻相引流锥的倾斜夹角为10～75°，所述副分离腔轻相引流锥的中间开有夹角为0～10°的副引流孔道，所述副引流孔道的直径为所述副分离腔直径的0.1～0.8倍。
本发明进一步设置为，所述主分离管的顶部设有主分离腔防冲帽，所述副分离管的顶部设有副分离腔防冲帽。
本发明进一步设置为，所述造旋器为导流叶片，所述导流叶片的螺旋倾角为10～75°；或者，所述造旋器为切向进口，所述切向进口的数量为1～6个。
本发明进一步设置为，所述主分离管的长度是内径的1～20倍，所述副分离管的长度是内径的1～20倍。
本发明进一步设置为，所述重相分离锥的倾角为10～75°、直径为所述副分离管内径的0.2～0.8倍。
本发明进一步设置为，每个所述主分离管的底部连接有一个分布管，所述分布管的的侧面共同连接有联通管，所述分布管的底部共同连接分配管，所述分配管的端部共同连接有分配罐，所述分配罐的底部连接有进口管。
本发明进一步设置为，所述分配管以所述分配罐的中心为圆心呈放射状沿径向均匀分布，数量为2～6根。
本发明进一步设置为，所述主副管联通管的截面为矩形或圆形，纵向分布2～8个，所述主副管联通管的长度b＝(D+d)/2+(10～200)mm；D是所述主分离管的内径，d是所述副分离管的内径。
本发明进一步设置为，如果所述一体化分离芯管有多个，则分布方式为以分配罐为中心成三角形、放射状或二者形状的结合均匀分布，分布圈数为1～6。
本发明提供的第二个技术方案如下：一种自适应多相一体化分离方法，所述分离方法包括如下步骤：
(1)待处理物料进入主分离管；
(2)通过主分离管内的旋流场作用，大气泡、大粒径油滴以及粘附在大气泡、大粒径油滴上的悬浮固体都是从顶部离开被去除；
(3)分离后的其余液相经过主副管联通管进入副分离管，通过副分离管切向造旋口后在副分离管内做旋转流动，进一步去除对小气泡、小粒径油滴以及粘附在所述小气泡、小粒径油滴上的剩余悬浮固体；
(4)分离后得到的洁净液相从重相分离锥周边排出。
本发明进一步设置为，所述大气泡尺寸为大于10μm，所述大粒径油滴尺寸为大于20μm，所述小气泡尺寸为5-10μm，所述小粒径油滴尺寸为10-20μm。
本发明进一步设置为，所述主分离管内处理主相的加速度为重力加速度的5～5000倍，所述副分离管内处理主相的加速度为重力加速度的10～10000倍。
本发明提供的第三个技术方案如下：一种自适应多相一体化分离方法，所述分离方法包括如下步骤：
(1)待处理物料经过进口管进入分配罐，经分配罐缓冲后，待处理物料进入分配管，物料通过分配管到达分布管，分布管间通过联通管相连确保物料的均匀分配，物料通过分布管进入一体化分离芯管；
(2)待处理物料先进入一体化分离芯管的主分离管，通过主分离管内的旋流场作用，去除大气泡、大粒径油滴以及粘附在大气泡、大粒径油滴上的悬浮固体；
(3)分离后的其余液相经过主副管联通管进入副分离管，通过副分离管切向造旋口后在副分离管内做旋转流动，进一步去除对小气泡、小粒径油滴以及粘附在所述 小气泡、小粒径油滴上的剩余悬浮固体；
(4)分离后得到的洁净液相从重相分离锥周边排出。
本发明进一步设置为，所述一体化分离芯管为单根或多根，一体化分离芯管压降≤0.3MPa。
综上所述，本发明具有以下有益效果：
(1)本发明通过主分离管与副分离管的耦合结构实现对油、气、浊的协同分离。
(2)本发明的油相脱除率和气相脱除率均大于90％，且处理量具有极高的操作弹性，与传统的旋流场分离方法相比，处理量具有极高的处理量操作弹性，为50％-150％，适用于对高含油、高含浊污水的紧凑处理，分离效率高，实现了短流程下紧凑、快速分离的目的，能够有效降低相关分离系统的占地面积，弥补了现有技术的不足。
(3)在本发明设计的流量操作弹性范围内，一体化分离芯管压降≤0.3Mpa。
附图说明
图1-1为自适应多相一体化分离装置的一种结构示意图；
图1-2为自适应多相一体化分离装置的另一种结构示意图；
图2为主分离管的结构示意图；
图3为副分离管的结构示意图；
图4-1到图4-4分别为副分离管数目为2(旋向与主分离管旋向相同)、2(旋向与主分离管旋向相反)、3(旋向与主分离管旋向相同)、3(旋向与主分离管旋向相反)的结构俯视图；
图5-1为导流叶片的结构示意图；
图5-2为旋转式导流叶片的结构示意图；
图6-1为一个切向进口的结构俯视图；
图6-2为三个切向进口的结构俯视图；
图7-1为多个一体化分离芯管的装配示意图(多个分布管，仅画了一个一体化分离芯管示意)；
图7-2为图7-1的部分结构俯视图；
图8-1为多个一体化分离芯管的装配示意图(单个分布管，仅画了一个一体化分 离芯管示意)；
图8-2为图8-1的部分结构俯视图；
图9-1到图9-3为一体化分离芯管的布管形式(分别为三角形布置、放射状布置、三角形结合放射状布置)。
图10为本发明立式设备中的安装结构示意图；
图11为本发明卧式设备中的安装结构示意图。
其中，1：主分离管；2：副分离管；3：主副管联通管；4：连接件。
1-1：造旋器；1-2：主分离腔；1-3：主分离腔轻相引流锥；1-4：主分离腔防冲帽；1-5、导流叶片；1-6、切向进口；1-7、主引流孔道。
2-1：副分离管切向造旋口；2-2：重相分离锥；2-3：副分离腔；2-4：副分离腔轻相引流锥；2-5：副分离腔防冲帽；2-6、副引流孔道。
0-1：一体化分离芯管；0-2：分布管；0-3：分配管；0-4：进口管；0-5：联通管；0-6：分配罐。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
实施例1
参见图1，一种自适应多相一体化分离装置，分离装置包括一根以上一体化分离芯管0-1，一体化分离芯管0-1包括主分离管1、副分离管2以及连通主分离管1和副分离管2的主副管联通管3，一个主分离管1的周围设有2个以上副分离管2。主分离管1的底部进口设有造旋器1-1，造旋器1-1产生的旋流场使流过主分离管1的液体由轴向运动变换为旋转运动。副分离管2沿轴向设有副分离管切向造旋口2-1，副分离管切向造旋口2-1使流过副分离管2的液体通过切向进入副分离管2做旋转运动。副分离管2内的底部设有锥形或凸台形的重相分离锥2-2。
进一步地，可在主分离管1的底部连接连接件4用于连接其他设备上或者管道上。参见图2，作为另一种自适应多相一体化分离装置的结构，可通过连接件4连接 其他的管道等。
参见图2和图3，主分离管1内为主分离腔1-2，副分离管2内为副分离腔2-3。主分离管1的上部设有主分离腔轻相引流锥1-3，副分离管2的上部设有副分离腔轻相引流锥2-4。
副分离管2的数量为1～6，副分离管2的流场旋向为顺时针或逆时针，与主分离管1的流场旋向相同或相反。其中，副分离管2的数量为2或3的结构可参见图4-1到图4-4。
主分离腔轻相引流锥1-3的倾斜夹角为10～75°，所述主分离腔轻相引流锥1-3上设有夹角为0～10°的主引流孔道1-7，主引流孔道1-7的直径为主分离腔1-2直径的0.1～0.8倍。副分离腔轻相引流锥2-4的倾斜夹角为10～75°，副分离腔轻相引流锥2-4上设有夹角为0～10°的副引流孔道2-6，副引流孔道2-6的直径为副分离腔1-2直径的0.1～0.8倍。
主分离管1的顶部设有用于防冲的主分离腔防冲帽1-4，副分离管2的顶部设有副分离腔防冲帽2-5。
参见图5-1和图5-2，造旋器1-1为导流叶片1-5，导流叶片1-5的螺旋倾角为10～75°。或者，参见图6-1和图6-2，造旋器1-1为切向进口1-6，切向进口1-6的数量为1～6个。
主分离管1的长度是内径的1～20倍，副分离管2的长度是内径的1～20倍。
重相分离锥2-2的倾角为10～75°、直径为副分离管2内径的0.2～0.8倍。
本实施例的物料分离过程如下：待处理物料进入主副腔组合的自适应脱气除油除浊一体化分离芯管0-1，实现油、气、浊的协同一体化分离；所述物料分离完成后经过立式容器缓冲，气相、含浊油相、处理后水通过相应接口对应外排。
实施例2
参见图7-1、图7-2、图8-1和图8-2，每个主分离管1的底部连接有一个分布管0-2，分布管0-2的侧面共同连接有联通管0-5，分布管0-2的底部共同连接分配管0-3，分配管0-3的端部共同连接有分配罐0-6，分配罐0-6为卧式或立式容器，分配罐0-6的底部连接有进口管0-4。
分配管0-3以分配罐0-6的中心为圆心呈放射状沿径向均匀分布，数量为2～6根。
主副管联通管0-5的截面为矩形或圆形，纵向分布2～8个，主副管联通管0-5的长度b＝(D+d)/2+(10～200)mm。D是主分离管1的内径，d是副分离管2的内径。
根据设备设计处理量不同设置一体化分离芯管0-1为单根或多根，如设备尺寸足够大，可布置多根。如果一体化分离芯管0-1有多个，则分布方式为以分配罐0-6为中心成三角形、放射状或二者形状的结合均匀分布，分布圈数为1～6，参见图9-1到图9-3。
参见图10和图11，本发明可安装在立式设备中或者卧式设备中。
本实施例的物料分离过程如下：待处理物料经过进口管0-4进入分配罐0-6；经分配罐0-6缓冲后，待处理物料进入周向均匀分布的分配管0-3；物料通过分配管0-3到达分布管0-2，分布管0-2间通过联通管0-5相连确保物料的均匀分配；物料通过分布管0-2进入主副腔组合的自适应脱气除油除浊一体化分离芯管0-1，实现油、气、浊的协同一体化分离；所述物料分离完成后经过立式容器缓冲，气相、含浊油相、处理后水通过相应接口对应外排。
实施例3
本实施例提供自适应一体化分离装置更具体的一种结构，一个立式罐体内设置多组并联的主副腔组合的分离器实现高效快速分离。
分配罐0-6为带椭圆形封头的圆筒形容器，按最大处理量运行0.3s可填充满整个分配罐0-6，3根分配管0-3以分配罐0-6中心为圆心呈放射状沿径向向外均匀分布，每相邻两根分配管0-3间夹角为120°。联通管0-5的内径为进口管0-4内径的0.8倍，分布管0-2内径与主分离管1内径保持一致，一体化分离芯管0-1共计使用40根，分布按三角形混合放射状分布排列，分布圈数选用3圈。进口管0-4尺寸中液相流速1.5m/s。
一体化分离芯管0-1中，连接件4用法兰连接。主分离腔1-2内流场旋向为顺时针。主副管联通管3采用矩形截面与主分离腔1-2和副分离腔2-3切向连接，截面积为副分离腔2-3截面积的0.5倍，主副管联通管3纵向均匀分布5根，主副管联通管3长度150mm，4个副分离腔2-3内流场旋向为顺时针。主分离管1的造旋器1-1使用旋向为顺时针的导流叶片1-5，叶片螺旋倾角β为45°。主分离管1内径为150mm，主分离管1长度为450mm，主分离腔轻相引流锥1-3倾斜夹角β2为30°，引流孔道1-7的夹角β1为3°，引流孔道1-7直径D1＝25mm，主分离腔防冲帽1-4安装在主分 离腔轻相引流锥1-3上部。副分离腔2-3的重相分离锥2-2布置于副分离腔2-3底部呈凸台形，其直径d2＝40mm，倾角为30°；副分离腔轻相引流锥2-4倾斜夹角γ2为20°。副分离管2内径为50mm，长度为300mm；引流孔道2-6的夹角γ1为3°，引流孔道2-6直径d1＝25mm；副分离腔防冲帽2-5安装于副分离腔轻相引流锥2-4上部。
在狭长空间内，通过四个直径为1800mm的立式罐体并联，实现了平台生产水处理能力24000m 3/d的扩容。设备进口生产水油含量平均2000mg/L，最高可达3000mg/L，设备进口为溶解气为饱和态，另外还体积比约10％的气相，含浊浓度在1000mg/L左右，经过设备处理后，水相出口油含量平均值低于150mg/L，最低可低于90mg/L，分离后气相脱除率＞95％，设备整体压降＜0.2MPa。
以上所述仅为本发明的较佳实施例，并不用以限制本发明，凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (15)

  1. 一种自适应多相一体化分离装置，其特征在于，所述分离装置包括一根以上一体化分离芯管，所述一体化分离芯管包括主分离管、副分离管以及连通所述主分离管和所述副分离管的主副管联通管，一个所述主分离管的周围设有2个以上所述副分离管；所述主分离管的底部进口设有造旋器，所述造旋器产生的旋流场使流过所述主分离管的液体由轴向运动变换为旋转运动；所述副分离管的沿轴向设有副分离管切向造旋口，所述副分离管切向造旋口使流过所述副分离管的液体通过切向进入副分离管做旋转运动；所述副分离管内的底部设有锥形或凸台形的重相分离锥。
  2. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，所述主分离管内为主分离腔，所述副分离管内为副分离腔；所述主分离管的上部设有主分离腔轻相引流锥，所述副分离管的上部设有副分离腔轻相引流锥。
  3. 根据权利要求2所述的自适应多相一体化分离装置，其特征在于，所述主分离腔轻相引流锥的倾斜夹角为10～75°，所述主分离腔轻相引流锥的中间开有夹角为0～10°的主引流孔道，所述主引流孔道的直径为所述主分离腔直径的0.1～0.8倍；所述副分离腔轻相引流锥的倾斜夹角为10～75°，所述副分离腔轻相引流锥的中间开有夹角为0～10°的副引流孔道，所述副引流孔道的直径为所述副分离腔直径的0.1～0.8倍。
  4. 根据权利要求2所述的自适应多相一体化分离装置，其特征在于，所述主分离管的顶部设有主分离腔防冲帽，所述副分离管的顶部设有副分离腔防冲帽。
  5. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，所述造旋器为导流叶片，所述导流叶片的螺旋倾角为10～75°；或者，所述造旋器为切向进口，所述切向进口的数量为1～6个。
  6. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，所述主分离管的长度是内径的1～20倍，所述副分离管的长度是内径的1～20倍。
  7. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，所述重相分离锥的倾角为10～75°、直径为所述副分离管内径的0.2～0.8倍。
  8. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，每个所述主分离管的底部连接有一个分布管，所述分布管的侧面共同连接有联通管，所述分布 管的底部共同连接分配管，所述分配管的端部共同连接有分配罐，所述分配罐的底部连接有进口管。
  9. 根据权利要求8所述的自适应多相一体化分离装置，其特征在于，所述分配管以所述分配罐的中心为圆心呈放射状沿径向均匀分布，数量为2～6根。
  10. 根据权利要求1所述的自适应多相一体化分离装置，其特征在于，所述主副管联通管的截面为矩形或圆形，纵向分布2～8个，所述主副管联通管的长度b＝(D+d)/2+(10～200)mm；D是所述主分离管的内径，d是所述副分离管的内径。
  11. 根据权利要求8所述的自适应多相一体化分离装置，其特征在于，如果所述一体化分离芯管有多个，则分布方式为以分配罐为中心成三角形、放射状或二者形状的结合均匀分布，分布圈数为1～6。
  12. 利用权利要求1-7任一项所述的自适应多相一体化分离装置进行分离的方法，其特征在于，所述分离方法包括如下步骤：
    (1)待处理物料进入主分离管；
    (2)通过主分离管内的旋流场作用，去除大气泡、大粒径油滴以及粘附在大气泡、大粒径油滴上的悬浮固体；
    (3)分离后的其余液相经过主副管联通管进入副分离管，通过副分离管切向造旋口后在副分离管内做旋转流动，进一步去除对小气泡、小粒径油滴以及粘附在所述小气泡、小粒径油滴上的剩余悬浮固体；
    (4)分离后得到的洁净液相从重相分离锥周边排出。
  13. 根据权利要求12所述的分离方法，其特征在于，所述大气泡尺寸为大于10μm，所述大粒径油滴尺寸为大于20μm，所述小气泡尺寸为5-10μm，所述小粒径油滴尺寸为10-20μm。
  14. 根据权利要求12所述的分离方法，其特征在于，所述主分离管内处理主相的加速度为重力加速度的5～5000倍，所述副分离管内处理主相的加速度为重力加速度的10～10000倍。
  15. 利用权利要求8-11任一项所述的自适应多相一体化分离装置进行分离的方法，其特征在于，所述分离方法包括如下步骤：
    (1)待处理物料经过进口管进入分配罐，经分配罐缓冲后，待处理物料进入分配管，物料通过分配管到达分布管，分布管间通过联通管相连确保物料的均匀分配， 物料通过分布管进入一体化分离芯管；
    (2)待处理物料先进入一体化分离芯管的主分离管，通过主分离管内的旋流场作用，去除大气泡、大粒径油滴以及粘附在大气泡、大粒径油滴上的悬浮固体；
    (3)分离后的其余液相经过主副管联通管进入副分离管，通过副分离管切向造旋口后在副分离管内做旋转流动，进一步去除对小气泡、小粒径油滴以及粘附在所述小气泡、小粒径油滴上的剩余悬浮固体；
    (4)分离后得到的洁净液相从重相分离锥周边排出。
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