WO2019024916A1 - 一种自适应变流量原油脱气的方法和装置 - Google Patents

一种自适应变流量原油脱气的方法和装置 Download PDF

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WO2019024916A1
WO2019024916A1 PCT/CN2018/098505 CN2018098505W WO2019024916A1 WO 2019024916 A1 WO2019024916 A1 WO 2019024916A1 CN 2018098505 W CN2018098505 W CN 2018098505W WO 2019024916 A1 WO2019024916 A1 WO 2019024916A1
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crude oil
degassing
liquid
tangential
inlet
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PCT/CN2018/098505
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French (fr)
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杨强
钱运东
黄燎云
徐道尉
张毅文
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上海米素环保科技有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0036—Flash degasification
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities

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  • the invention relates to the field of gas-liquid separation equipment, in particular to the technical field of oil and gas production equipment, in particular to a method and a device for adaptive de-gasification of variable-flow crude oil.
  • the crude oil extracted from oil wells is rich in various impurities such as gas, liquid and solid. Before the crude oil is transported, it needs to be de-sand, degassing and dehydration.
  • the physical technology of two-phase or three-phase separation mainly includes gravity settlement. , cyclone separation, coalescence filtration, membrane separation and other methods.
  • gas, liquid, and solid phase materials can be separated, but the separation takes a long time, and the conditions of fluctuations in the content of each component in crude oil production are not well adapted, resulting in unstable operation.
  • coalescence filtration is separated by permeability, the adaptation range is narrow, and there is a problem of short service life.
  • the same membrane separation also has problems such as easy pollution, short service life, easy clogging, etc.
  • the cyclone separation technology is suitable for inclusion.
  • Patent: CN201610704875.9 discloses a gravity sedimentation gas-liquid separation method, which combines gravity separation and membrane separation methods for oil and gas separation, and has the disadvantages of large equipment size and long processing time;
  • Patent: 200880102068.3 discloses The seed membrane separation method and the membrane separation device can reduce the adsorption of the membrane contaminant contained in the water to be treated on the membrane surface when the membrane is separated from the water to be treated, and the disadvantage is that the membrane is easily clogged and has a short service life.
  • the present invention provides a method and an apparatus for adaptively degassing a variable flow crude oil, and the specific technical solutions are as follows:
  • An adaptive variable flow crude oil degassing device comprising a tank body, a main flow tube and a plurality of pressure gradient degassing tubes distributed around the same, wherein each of the pressure gradient degassing tubes is provided with a plurality of tangential inlets ;
  • the can body has a cylindrical shape or a rectangular tube shape, and has a solid phase outlet at a bottom thereof, a liquid phase outlet at a bottom side wall thereof, a gas phase outlet at a top thereof, and a liquid inlet to be treated at a lower portion thereof.
  • a liquid level gauge is disposed at an axial position thereof;
  • the main flow tube is disposed at an intermediate position of the tank body, and is provided with a wind generator at an inlet thereof, and a main flow inverted cone is disposed near the end thereof, and at least one row of tangential outlets is disposed around the cylinder wall;
  • the pressure gradient degassing tube is disposed around the main flow tube, and has a row of tangential inlets on the axial wall surface thereof, and an inverted cone and a liquid solid phase outlet at the bottom thereof, and a gas phase outlet at the top thereof, and the gas phase outlet is disposed outside There is a shock-proof cup.
  • the invention also provides a method for efficiently degassing an adaptive variable flow crude oil, comprising the following steps:
  • a wind generator 2 is arranged at the inlet of the main pipe, and the number of rotations of the crude oil after passing through the wind generator is 1.3 to 5;
  • the crude oil having the number of rotations of 1.3 to 5 in the step (2) enters the pressure gradient degassing tube 10 through the tangential inlet distributed in the axial direction of the pressure gradient degassing tube, and the gas in the crude oil is gradually removed by the pressure gradient.
  • the removed gas is discharged through the pressure gradient degassing tube gas outlet 9, and the liquid phase containing the solid is discharged into the tank through the liquid phase outlet of the pressure gradient degassing tube;
  • (1)Adopting variable flow degassing device, multi-stage inlet and outlet can adapt to the liquid rotation speed caused by flow fluctuation, too high or too low, maintain the stability of degassing efficiency, especially suitable for flow fluctuation during crude oil exploitation It can reduce the impact on downstream instruments and equipment, realize fast and efficient degassing function, automatic liquid level control function, reduce the pressure of downstream equipment, simple structure and convenient installation, which can effectively reduce the floor space and make up for the shortcomings of the prior art.
  • FIG. 1 is a schematic structural view of a device of Embodiment 1;
  • Figure 2 is a schematic view of a tangential inlet of a pressure gradient degassing tube
  • FIG. 3 is a schematic diagram of a combination of a main flow tube and a pressure gradient degassing tube; wherein (a) is a schematic diagram of a connection manner in which the tangential inlets of the pressure gradient degassing tubes are combined in a clockwise direction, and (b) is a tangential inlet of the pressure gradient degassing tube.
  • FIG. 1 it mainly includes: 1 equipment inlet; 2 generator; 3 main tube inverted cone; 4 mainstream tube; 5 pressure gradient degassing tube gas outlet; 6 equipment gas outlet; 7 anti-flush cup; Gradient degassing tube tangential inlet; 9 pressure gradient degassing tube gas phase outlet; 10 pressure gradient degassing tube; 11 liquid level controller; 12 pressure gradient degassing tube inverted cone; 13 pressure gradient degassing tube liquid outlet; 14 equipment liquid phase outlet; 15 equipment solid phase outlet; 16 tanks.
  • Crude oil with a gas content fluctuation in the range of 5-20% and a flow rate in the range of 80-140 m 3 /h is passed from the equipment inlet 1 through the connecting pipe into the main flow pipe 4; at the inlet of the main flow separation pipe, a regenerator 2 is disposed, and the crude oil passes through After the spinner, the number of rotations is 1.3 ⁇ 5, and the gas is degassed through the pressure gradient degassing tube into the pressure gradient degassing tube. The gas is removed step by step under the pressure gradient, and the removed gas is discharged through the pressure gradient degassing tube gas outlet 8 The solid-liquid phase is discharged through the liquid phase outlet of the pressure gradient degassing tube, and the gas removal rate in the crude oil is not less than 96%.
  • the special structure of the vortexer, the inverted cone and the pressure gradient degassing tube in the main flow tube is tangentially connected to the inlet.
  • the number of liquid phase rotations in the pressure gradient degassing tube is 2-6, and enters the pressure gradient degassing tube. Crude oil achieves stable and efficient degassing.
  • the separated gas phase and liquid phase are discharged from the separator and then enter the tank body. Finally, the gas phase is discharged through the gas phase outlet 6 of the equipment, the liquid phase is discharged through the liquid phase outlet 13 of the equipment, and the solid phase is discharged through the solid phase outlet 14 of the equipment; The discharge flow rate of the liquid phase and the liquid phase are controlled by the liquid level controller, and the outlet flow rate is stable.
  • the gas removal rate in the crude oil is greater than 99%, and the solid removal rate is 99.9%.
  • FIG. 2 it is a schematic diagram of a pressure gradient degassing tube, wherein N1, N2, N3, and N4 are schematic diagrams of a tangential inlet of a single pressure gradient degassing tube in Embodiment 1.
  • (a) is a schematic diagram of a connection mode in which the shunt distributors are combined in a clockwise direction
  • (b) is a schematic diagram of a connection mode in which the shunt distributors are combined in a counterclockwise direction.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Cyclones (AREA)
  • Degasification And Air Bubble Elimination (AREA)

Abstract

本发明涉及一种自适应变流量原油脱气方法与装置。一种自适应变流量原油脱气装置包括壳体、主流分离管以及分布在其周围的分流分离管，所述分流分离管通过分流管与主流分离管连通；本发明通过对主流分离管与分流分离管进行特殊的组合，能够自适应入口原油流量波动，对于流量变化时，由主流分离器中的造旋器、倒锥以及分流管的特殊结构，分流分离管时刻均处于允许的工况条件下，保证了进入分流分离管中的原油脱气高效进行，实现了快速高效脱气功能、液面自动调节功能，减小下游设备压力，结构简单且安装方便，能够有效减少占地面积，弥补了现有技术的不足。

Description

一种自适应变流量原油脱气的方法和装置 技术领域
本发明涉及气液分离设备领域，特别涉及油气开采设备技术领域，具体的涉及一种自适应变流量原油脱气的方法与装置。
背景技术
油井开采出的原油富含气、液、固等多种杂质，在原油外输之前，需进行除砂、脱气、脱水等环节，目前进行两相或三相分离的物理技术主要有重力沉降、旋流分离、聚结过滤、膜分离等方法。对于重力沉降来说，能够分离气、液、固相物质，但分离所需时间长，且对原油开采中各组分含量波动较大的工况不能很好适应，造成操作不稳定的情况时有发生；聚结过滤通过渗透性进行分离，适应范围较窄，同时存在使用寿命短的问题，同样膜分离也存在易污染、使用寿命不长、易堵塞等问题；旋流分离技术适用于含大量(油)水的快速去除过程，但对某一个特定的旋流器来说，必须工作在一定的进口流量下才能稳定的发挥作用，具有一定的局限性。
专利：CN201610704875.9公开了一种重力沉降式气液分离方法，该专利结合重力分离和膜分离的方法进行油气分离，其缺点是设备尺寸较大，处理时间较长；专利：200880102068.3公开了一种膜分离方法及膜分离装置，在对被处理水进行膜分离处理时，可以降低被处理水中所含的膜污染物质在膜表面的吸附，其缺点是膜易堵塞、使用寿命短。
因此需要采用成本低、易操作、适应变工况且高效率的原油脱气的方法和设备对目前的技术进行优化。
发明内容
为了克服上述现有技术的不足，本发明提供了一种自适应变流量原油高效脱气的方法与装置，具体的技术方案如下：
一种自适应变流量原油脱气装置，包括罐体、主流管以及分布在其周围的多个压力梯度脱气管，其特征在于，所述每个压力梯度脱气管均设置有多个切向进口；
所述罐体为圆筒形或方筒形，在其底部设置有固相出口，在其底部侧壁设置有液相出口，在其顶部设置有气相出口，在其中下部设置有待处理液体入口，在其轴向位置设置有液位计；
所述主流管设置在罐体中间位置，在其入口处设置有造旋器，在其靠近末端处设置有主流倒锥，在其筒壁四周设置有至少一列切向出口；
所述压力梯度脱气管设置在主流管四周，在其轴向壁面上开有一列切向进口，在其底部设置有倒锥及液固相出口，在其顶部设置有气相出口，气相出口外设置有防冲挡杯。
本发明还提供了一种自适应变流量原油高效脱气的方法，包括如下步骤：
(1)原油由设备入口1经过连接管道进入主流管4；
(2)在主流管入口处设置造旋器2，原油经过造旋器后旋转数为1.3～5；
(3)步骤(2)中旋转数为1.3～5的原油通过分布在压力梯度脱气管轴线方向的切向入口进入压力梯度脱气管10，原油中气体在压力梯度作用下逐级脱除，脱除的气体经压力梯度脱气管气体出口9排出，含固体的液相经压力梯度脱气管液相出口排入罐体中；
(4)对步骤(5)中气相及液相的排出流量由液位控制器进行控制。
本发明的有益效果在于：
(1)采用自适应变流量脱气装置，多级进出口能够适应因流量波动而造成的液体旋转速度过高或过低，维持脱气效率的稳定，特别适应于原油开采过程中的流量波动，减小对下游仪器设备的冲击，实现快速高效脱气功能、液面自动控制功能，减小下游设备压力，结构简单且安装方便，能够有效减少占地面积，弥补了现有技术的不足。
附图说明
图1是实施例1的装置结构示意图；
图2是压力梯度脱气管切向进口示意图；
图3是主流管与压力梯度脱气管的组合方式示意图；其中，(a)是压力梯度脱气管切向进口均为顺时针方向组合的连接方式示意图，(b)是压力梯度脱气管切向进口均为逆时针方向组合的连接方式示意图；
符号说明：
1设备入口；2造旋器；3主流管倒锥；4主流管；
5压力梯度脱气管气相出口；6设备气相出口；7防冲挡杯；8压力梯度脱气管切向进口；9压力梯度脱气管气相出口；10压力梯度脱气管；11液位控制器；12压力梯度脱气管倒锥；13压力梯度脱气管液相出口；14设备液相出口；15设备固相出口；16罐体。
具体实施方式
下面，通过实施例对本发明进行具体描述。有必要在此指出的是，以下实施例只用于对本发明作进一步说明，不能理解为对本发明保护范围的限制，该领域的专业技术人员根据本发明的内容作出的一些非本质的改进和调整，仍属于本发明的保护范围。
实施例1
本申请的发明人经过广泛而深入的研究后发现，对于原油开采过程中最经济、最有效的脱气方法是采用旋流离心分离。基于研究，分离器入口形状及位置、几何尺寸、等都影响分离器的适用范围及分离精度，而流量的变化会导致入口速度变化，进而影响分离效果，由此可知要想在流量变化的情况下利用旋流离心分离实现分离效果，就必须随流量变化增加或减少分离器的数量，以保证分离器工作在合理的工况下，然而在实际工作中通过改变分离器数量并不是一件简单的事情。基于以上发现，本发明得以完成。
如图1所示，其主要包括：1设备入口；2造旋器；3主流管倒锥；4主流管；5压力梯度脱气管气相出口；6设备气相出口；7防冲倒杯；8压力梯度脱气管切向进口；9压力梯度脱气管气相出口；10压力梯度脱气管；11液位控制器；12压力梯度脱气管倒锥；13压力梯度脱气管液相出口；14设备液相出口；15设备固相出口；16罐体。
含气率在5～20％范围波动、流量在80～140m 3/h范围内波动的原油由设备入口1经过连接管道进入主流管4；在主流分离管入口处设置造旋器2，原油经过造旋器后旋转数为1.3～5，通过压力梯度脱气管切向进口进入压力梯度脱气管中，在压力梯度作用下气体逐级脱除，脱除的气体经压力梯度脱气管气相出口8排出，含固液相经压力梯度脱气管管液相出口排出，此时原油中气体脱除率不小于96％。
对于流量变化时，由主流管中的造旋器、倒锥以及压力梯度脱气管切向进口的特殊结构，压力梯度脱气管中的液相旋转数为2～6，进入压力梯度脱气管中的原油实现了稳定高效的脱气。
分离出的气相和液相均从分离器中排出后进入到罐体中，最后气相经设备气相出口6排出，液相经设备液相出口13排出，固相经设备固相出口14排出；气相及液相的排出流量由液位控制器进行控制，出口流量平稳。
经过本设备后，原油中气体脱除率大于99％，固体脱除率99.9％。
如图2所示，是压力梯度脱气管示意图，其中N1、N2、N3、N4为实施例1中单根压力梯度脱气管切向进口示意图。
如图3所示，其中，(a)是分流分布器均为顺时针方向组合的连接方式示意图，(b)是分流分布器均为逆时针方向组合的连接方式示意图。

Claims (7)

  1. 一种自适应变流量原油脱气装置，其特征在于，包括罐体、主流管以及分布在其周围的多个压力梯度脱气管，其特征在于，所述每个压力梯度脱气管均设置有多个切向进口；
    所述罐体为圆筒形或方筒形，在其底部设置有固相出口，在其底部侧壁设置有液相出口，在其顶部设置有气相出口，在其中下部设置有待处理液体入口，在其轴向位置设置有液位计；
    所述主流管设置在罐体中间位置，在其入口处设置有造旋器，在其靠近末端处设置有主流倒锥，在其筒壁四周设置有至少一列切向出口；
    所述压力梯度脱气管设置在主流管四周，在其轴向壁面上开有一列切向进口，在其底部设置有倒锥及液固相出口，在其顶部设置有气相出口，气相出口外设置有防冲挡杯。
  2. 如权利要求1所述的一种自适应变流量原油脱气装置，其特征在于，所述造旋器为中间圆柱及其四周导流叶片组成或者将导流叶片置于主流倒锥上，所述导流叶片螺旋角有15°～20°、20°～40°、40°～60°三种规格，其旋向为左旋或右旋。
  3. 如权利要求1所述的一种自适应变流量原油脱气装置，其特征在于，所述倒锥锥角为45°～60°。
  4. 如权利要求1所述的一种自适应变流量原油脱气装置，其特征在于，所述每列切向出口从主流管底部到顶部设置多级，所述切向入口从压力梯度脱气管底部到顶部设置多级，所述每级切向出口和切向入口由连接管依次连通，切向出口方向与造旋器导流叶片旋向一致，切向入口方向为顺时针或逆时针方向。
  5. 一种自适应变流量原油脱气方法，其步骤为，待处理原油液体经泵加压后由装置入口进入，随后经入口连接管进入主流管，待处理液在造旋器处经导流叶片后开始在主流管内高速旋转上升，随后经过各级切向出口和切向入口进入到压力梯度脱气管中，在离心力和重力作用下气液分离，分离后的气体有气体出口排出，分离后的液体由液相出口排出，少量的固体经固相出口排出。
  6. 如权利要求5所述的一种自适应变流量原油脱气方法，其特征在于，所 述导流叶片产生的高速旋转液体周向速度与轴向速度之比为1.5～4。
  7. 如权利要求5所述的一种自适应变流量原油脱气方法，其特征在于，所述每级切向入口液体流速为2.6m/s～4.4m/s、4.4m/s～6.7m/s、6.7m/s～9.3m/s，分别对应三种导流叶片螺旋角以及0.01MPa～0.05MPa、0.05MPa～0.1MPa、0.1MPa～0.3MPa三种压力降。
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