WO2019024915A1 - 一种海上气田平台生产水处理方法及其装置 - Google Patents

一种海上气田平台生产水处理方法及其装置 Download PDF

Info

Publication number
WO2019024915A1
WO2019024915A1 PCT/CN2018/098504 CN2018098504W WO2019024915A1 WO 2019024915 A1 WO2019024915 A1 WO 2019024915A1 CN 2018098504 W CN2018098504 W CN 2018098504W WO 2019024915 A1 WO2019024915 A1 WO 2019024915A1
Authority
WO
WIPO (PCT)
Prior art keywords
oil
coalescing
production
degreasing
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2018/098504
Other languages
English (en)
French (fr)
Inventor
杨强
卢浩
刘懿谦
李跃喜
朱凯
李劲松
张万兵
曾伟
朱光辉
谢斌
欧世兴
安海重
李毅
杜帅
江陵
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
East China University of Science and Technology
Yacheng Operation Co of CNOOC China Ltd
Original Assignee
East China University of Science and Technology
Yacheng Operation Co of CNOOC China Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by East China University of Science and Technology, Yacheng Operation Co of CNOOC China Ltd filed Critical East China University of Science and Technology
Publication of WO2019024915A1 publication Critical patent/WO2019024915A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)

Definitions

  • the invention relates to a sewage degreasing treatment method and a device used for realizing the same, and belongs to the environmental protection field of oil sewage treatment, and is particularly suitable for degreasing treatment of offshore production oil and gas production platform.
  • the underground gas field is produced by high-temperature and high-pressure oil, water and gas three-phase mixture.
  • the produced material is cooled by the heat exchanger, and then the oil, water and gas are separated by the production separator. The separated oil and gas are further.
  • the external storage will be discharged, and the separated production water will be discharged to the sea after degreasing treatment.
  • the oil content of the produced water in the sea should reach the environmental standard of the corresponding sea area.
  • the separation of oil and water in the production separator is simply gravity. Settling or strengthening gravity sedimentation, so the effluent from the production separator contains a large amount of emulsified oil.
  • the existing production water treatment process in the offshore gas field is as follows: the effluent from the production separator enters the hydrocyclone, and the effluent after the cyclone separation enters the flash tank to buffer the sea. Therefore, the separation performance of the hydrocyclone directly determines the degreasing effect of the produced water. Due to the limitation of the cyclone separation mechanism, the separation accuracy of the hydrocyclone is 10 um or more, and there is almost no separation effect on the oil droplets less than 10 um.
  • the downhole pressure is reduced, the production and production operation pressures are reduced, the gas phase flow rate is increased, the emulsification caused by the heat exchange phase transformation and pipeline transportation is more serious, and the particle size distribution of the oil droplets in the production water is changed.
  • Small there are a large number of oil droplets with a particle size of less than 10um, which exceeds the separation ability of existing processes and equipment, resulting in serious water and oil content in the sea.
  • the present invention provides a method and a device for upgrading and reforming the production water treatment process by using the high-efficiency deep coalescence and degreasing technology, so as to achieve the purpose of stable treatment of the dewatering of the production water and the discharge of the standard. .
  • the technical idea of the method part of the invention is that the relationship between the coalescing and degreasing device and the hydrocyclone can be either series or parallel, and the switching between series and parallel is determined by the operating conditions of the production separator, combined with hydraulic power.
  • the cyclone has a fast separation function for oil droplets above 10um and a deep dewatering function of the coalescing and degreasing device for emulsified oil droplets below 10um.
  • the invention can effectively adapt to the fluctuating conditions in the process operation.
  • a method for producing water treatment in an offshore gas field platform, adding a coalescing and degreasing device on the basis of the original production water treatment process, the device replacing the original production water booster pump and the hydrocyclone in parallel, or in series after the hydrocyclone ; includes the following process steps:
  • Step (1) when the effluent oil content of the production separator is less than 5000 mg/L, the coalescing and degreasing device replaces the production water booster pump and the hydrocyclone, and the effluent of the production separator directly enters the coalescence
  • the purified water after coalescence and degreasing enters the flash tank and is discharged into the sea after degassing and buffering, and the condensed oil after coalescence and degreasing is discharged into the recovery oil tank;
  • Step (2) when the effluent oil content of the production separator is higher than 5000 mg/L, the coalescing and degreasing device is connected in series after the hydrocyclone, and the effluent of the production separator enters the hydrocyclone through the production water boosting pump
  • the slick oil after swirling and degreasing is discharged into the recovery oil tank, and the production water after the cyclone deoiling enters the coalescing and degreasing device, and the purified water after coalescence and degreasing enters the flash tank, and after coalescence and degreasing
  • the slop oil is discharged into the recovery tank.
  • the oil content in the production water after the cyclone deoiling by the hydrocyclone in step (2) is less than 1000 mg/L.
  • the production separator effluent according to the steps (1) and (2) is a liquid containing no or a small amount of solid particles or sludge, and if the production separator effluent contains a large amount of solid particles or sludge, the production separator and Adding a solid filter with an accuracy of 10 to 50 um between the coalescing and degreasing devices, the filtration efficiency of the solid filter for solid particles above 50 um is not less than 95%; the coalescing module in the coalescing and degreasing device Solid particles of less than 50 um may be allowed to pass.
  • step (1) and step (2) the internal support of the coalescing and degreasing device has a certain pressure difference bearing strength, and a pressure difference overload protection is required on the inlet and outlet pipes of the coalescing and degreasing device, and when the instantaneous pressure difference exceeds 1.5 MPa, The coalescing degreaser outlet valve is automatically closed.
  • a coalescing and degreasing device for realizing the separation method according to any of the above methods, wherein a coalescing and degreasing device is added on the basis of the original production water treatment process, and the device is used in parallel to replace the original production water booster pump and the hydrocyclone, or in series After the hydrocyclone;
  • the coalescing and degreasing device comprises a tank body and a oil pack, an inlet distributor, a rectifier, a preliminary coalescing separation module, a deep coalescing separation module, and a strengthening settling module;
  • the effluent oil content of the production separator in the step (1) is less than 2000 mg/L
  • the coalescing and degreasing device is provided with a first-stage oil pack, and the internal water flow direction of the device is sequentially passed through the inlet.
  • the effluent oil content of the production separator in the step (1) is 2000-5000 mg/L
  • the coalescing and degreasing device is provided with two-stage oil packs, and the flow direction of the production water in the device is sequentially After the inlet distributor, rectifier, preliminary coalescence separation module, and enhanced settling module, the separated oil is discharged into the first oil pack, and the separated water continues to flow through the deep coalescing separation module, the enhanced sedimentation module, and finally separated. The oil enters the secondary oil pack and the separated production water is discharged from the device outlet.
  • the primary or secondary oil pack of the coalescence and degreasing device is automatically controlled by the boundary-control valve linkage, and the oil is intermittently discharged.
  • the cross-sectional flow velocity of the fluid in the coalescing and degreasing device is from 0.008 to 0.02 m/s, and the preliminary coalescence and the deep coalescing module are laminar.
  • the preliminary coalescence separation module has a volume specific surface area of 7000 to 15000 m 2 /m 3 , a void ratio of 0.75 to 0.85, a module depth of 200 to 400 mm, a pressure drop of less than 0.06 Mpa, and a separation precision of 10 ⁇ m.
  • the efficiency is not less than 80%.
  • FIG. 2 is a schematic structural view of a first-stage oil-pack coalescence and degreasing device of Embodiment 1;
  • FIG. 3 is a schematic structural view of a two-stage oil-pack coalescence and degreasing device.
  • a method for producing water treatment in an offshore gas field platform comprising the following process steps:
  • Step (1) When the effluent oil content of the production separator 11 is less than 5000 mg/L, the coalescing and degreasing device replaces the production water booster pump 12 and the hydrocyclone 13, and the effluent of the production separator directly enters the The coalescing and degreasing device is described, and the purified water after coalescence and degreasing enters the production water flash tank 14 and is deaerated and buffered, and discharged into the recovery oil tank after coalescence and degreasing;
  • Step (2) when the effluent oil content of the production separator is higher than 5000 mg/L, the coalescing and degreasing device is connected in series after the hydrocyclone, and the effluent of the production separator enters the hydrocyclone through the production water boosting pump
  • the slick oil after swirling and degreasing is discharged into the recovery oil tank, and the production water after the cyclone deoiling enters the coalescing and degreasing device 110, and the purified water after coalescence and degreasing enters the production water flash tank, and coalesces
  • the oil after the oil is discharged into the recovery tank.
  • the oil content in the production water after the cyclone deoiling by the hydrocyclone in step (2) is less than 1000 mg/L.
  • the production separator effluent according to the steps (1) and (2) is a liquid containing no or a small amount of solid particles or sludge, and if the production separator effluent contains a large amount of solid particles or sludge, the production separator and Adding a solid filter 19 with an accuracy of 10 to 50 um between the coalescing and degreasing devices, the solid filter has a filtration efficiency of not less than 95% for solid particles of 50 um or more; agglomeration in the coalescing and degreasing device
  • the module can allow solid particles of less than 50um to pass.
  • step (1) and step (2) the internal support of the coalescing and degreasing device has a certain pressure difference bearing strength, and a pressure difference overload protection is required on the inlet and outlet pipes of the coalescing and degreasing device, and when the instantaneous pressure difference exceeds 1.5 MPa, The coalescing degreaser outlet valve is automatically closed.
  • a coalescing and degreasing device for realizing the separation method of any of the above, the coalescing and degreasing device comprising a tank body and a oil pack, an inlet distributor 21, a rectifier 22, a preliminary coalescing separation module 23, and a deep coalescence separation Module 24, enhanced settling module 25;
  • the effluent oil content of the production separator in the step (1) is less than 2000 mg/L
  • the coalescing and degreasing device is provided with a first-stage oil pack, and the internal water flow direction of the device is sequentially passed through the inlet.
  • the effluent oil content of the production separator in the step (1) is 2000-5000 mg/L
  • the coalescing and degreasing device is provided with two-stage oil packs, and the flow direction of the production water in the device is sequentially After the inlet distributor, the rectifier, the preliminary coalescing separation module, and the enhanced settling module, the separated oil is discharged into the first oil pack 26, and the separated water continues to flow through the deep coalescing separation module, the strengthening settling module, and finally the separation.
  • the discharged oil is discharged into the secondary oil pack 39, and the separated production water is discharged from the device outlet.
  • the primary or secondary oil pack of the coalescence and degreasing device is automatically controlled by the boundary-control valve linkage, and the oil is intermittently discharged.
  • the cross-sectional flow velocity of the fluid in the coalescing and degreasing device is from 0.008 to 0.02 m/s, and the preliminary coalescence and the deep coalescing module are laminar.
  • the preliminary coalescence separation module has a volume specific surface area of 7000 to 15000 m 2 /m 3 , a void ratio of 0.75 to 0.85, a module depth of 200 to 400 mm, a pressure drop of less than 0.06 Mpa, and a separation precision of 10 ⁇ m.
  • the efficiency is not less than 80%.
  • the deep coalescing separation module has a volume specific surface area of 20,000 to 24000 m 2 /m 3 , a void ratio of 0.71 to 0.69, a module depth of 200 to 400 mm, a pressure drop of less than 0.2 MPa, and a separation precision of 2 um.
  • the efficiency is not less than 95%.
  • the material used for the metal skeleton fiber in the preliminary coalescing separation module and the deep coalescing separation module can be used when the chloride ion content in the production water is less than 1000 mg/L. 316L or 904L fiber; when the chloride ion oil in the production water is higher than 2000mg/L, the metal skeleton fiber material must be titanium alloy fiber.
  • the operating state of the process is: treatment capacity 15m 3 /h; production water contains trace solid particles, chloride ion content 2000mg / L; production separator effluent oil content less than 1500mg / L, oil droplet size distribution range 1 ⁇ 100um
  • the median particle size is 12um; the hydrocyclone separation efficiency is about 80%; the seawater production water and oil content is about 300mg/L.
  • Solution choice increase the pre-solid filter; in normal operation, the coalescing and degreasing device directly replaces the production water booster pump 12 and the hydrocyclone 13; using a first-stage oil-pack coalescence and degreasing device, the structure of the device is shown in Figure 2.
  • the inner diameter of the device is 600 mm; the preliminary coalescence separation module 23 has a volume specific surface area of 12000 m 2 /m 3 , the module depth is 400 mm, the metal skeleton fiber is a titanium alloy, and the deep coalescence separation module 24 has a volume specific surface area of 22000 m 2 /m 3 , the module The depth is 400mm, the metal skeleton fiber is titanium alloy; the depth of the strengthening settling module 25 is 200mm; the oil pack 26 is provided with a boundary to automatically control the oil discharge.
  • the oil content in the production water can be stably reduced to less than 30mg/L, which ensures the discharge of the produced water, which proves that the modification method and device have good application effect.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Removal Of Floating Material (AREA)
  • Physical Water Treatments (AREA)

Abstract

一种海上气田平台生产水处理装置，在原生产水处理流程的基础上利用增加了高效深度聚结除油装置（110），该装置（110）既可以并联替代原生产水增压泵（12）和水力旋流器（13），又可以串联在水力旋流器（13）之后；该装置可将外排生产水含油量从几千降低至30mg/L以内，确保了生产水的达标外排，适合在海上采油、采气平台上推广使用。还公开了一种海上气田平台生产水处理方法。

Description

一种海上气田平台生产水处理方法及其装置 技术领域
本发明涉及一种污水除油的处理方法及实现该方法所用的装置，属于油类污水处理的环保领域，尤其适用于海上采油、采气平台外排生产水的除油处理。
背景技术
海上气田井下采出物为高温高压的油、水、气三相混合物，采出物先经换热器降温，然后经生产分离器将油、水、气三相分离；分离后的油和气进一步处理后外输存储，分离后的生产水经除油处理后排海，排海生产水的油含量需达到对应海域的环保标准。
由于采出物在经换热器降温发生相变的过程中会发生严重的乳化，从而形成油包水和水包油型乳状液，而生产分离器中对油和水的分离只是简单的重力沉降或强化重力沉降，因此生产分离器的出水中含有大量的乳化油。而海上气田现有生产水处理流程为：生产分离器出水进入水力旋流器，旋流分离后的出水进入闪蒸罐缓冲后排海。因此，水力旋流器的分离性能直接决定了生产水的除油效果，由于旋流分离机理的限制，水力旋流器的分离精度为10um以上，对小于10um的油滴几乎无分离作用。
随着气田开采进入中期以后，井下压力降低、采出物和生产操作压力降低、气相流量增大，在换热相变和管道传输过程中造成的乳化更加严重，生产水中油滴粒径分布变小，出现大量粒径小于10um的油滴，超出了现有工艺和设备的分离能力，从而造成排海生产水油含量严重超标。
发明内容
针对现有工艺及设备的不足，本发明运用高效深度聚结除油技术，提供了一种生产水处理工艺的升级改造方法及装置，以达到对生产水除油的稳定处理并达标排放的目的。
本发明中方法部分的技术构思为：聚结除油装置与水力旋流器的关系既可以为串联又可以为并联，串并联之间的切换由生产分离器的运行工况决定，结 合了水力旋流器对10um以上油滴的快速分离功能和聚结除油装置对10um以下乳化油滴的深度高效除油功能，该发明能有效适应工艺运行中的波动工况。
具体技术方案如下：
一种海上气田平台生产水处理的方法，在原生产水处理流程的基础上增设聚结除油装置，该装置并联替代原生产水增压泵和水力旋流器，或串联在水力旋流器之后；包括以下工艺步骤：
步骤(1)：当生产分离器的出水油含量低于5000mg/L时，聚结除油装置替代生产水增压泵和水力旋流器，所述生产分离器的出水直接进入所述聚结除油装置，聚结除油后的净化水进入闪蒸罐脱气缓冲后排海，聚结除油后的污油排入回收油罐；
步骤(2)：当生产分离器的出水油含量高于5000mg/L时，聚结除油装置串联在水力旋流器之后，所述生产分离器的出水经生产水增压泵进入水力旋流器，旋流除油后的污油排入回收油罐，旋流除油后的生产水进入聚结除油装置，聚结除油后的净化水进入闪蒸罐，聚结除油后的污油排入回收油罐。
步骤(2)中所述经水力旋流器旋流除油后的生产水中油含量小于1000mg/L。
步骤(1)和步骤(2)所述生产分离器出水为不含或含微量固体颗粒或油泥的液体，若所述生产分离器出水含有大量固体颗粒或油泥，则在所述生产分离器和所述聚结除油装置之间增加10～50um精度的固体过滤器，所述固体过滤器对50um以上固体颗粒的过滤效率不低于95％；所述聚结除油装置内的聚结模块可以允许小于50um的固体颗粒通过。
步骤(1)和步骤(2)所述聚结除油装置内部支架具有一定压差承受强度，需在聚结除油装置进出口管路上设置压差过载保护，瞬时压差超过1.5MPa时，聚结除油装置出口阀门自动关闭。
一种实现上述任一所述分离方法的聚结除油装置，在原生产水处理流程的基础上增设聚结除油装置，该装置并联替代原生产水增压泵和水力旋流器，或串联在水力旋流器之后；所述聚结除油装置包括罐体和油包、入口分布器、整流器、初步聚结分离模块、深度聚结分离模块、强化沉降模块；
在一个优选的实施方式中，步骤(1)中所述生产分离器的出水油含量小于2000mg/L，所述聚结除油装置设置一级油包，装置内部生产水延流动方向依次 经过入口分布器、整流器、初步聚结分离模块、深度聚结分离模块、强化沉降模块，然后分离后的油进入一级油包排出，分离后的生产水由装置出水口排出；
在另一个优选的实施方式中，步骤(1)中所述生产分离器的出水油含量2000～5000mg/L，所述聚结除油装置设置两级油包，装置内生产水延流动方向依次经过入口分布器、整流器、初步聚结分离模块、强化沉降模块，然后分离出的油进入一级油包排出，分离后的水再继续流经深度聚结分离模块、强化沉降模块，最后分离出的油进入二级油包排出，分离出的生产水由装置出水口排出。
较佳的，所述聚结除油装置的一级或二级油包都采用界位-控制阀联动自动控制，间断式排油。
较佳的，所述聚结除油装置内流体截面流速为0.008～0.02m/s，所述初步聚结和所述深度聚结模块内为层流机理。
较佳的，所述初步聚结分离模块的体积比表面积为7000～15000m 2/m 3、空隙率为0.75～0.85、模块深度为200～400mm、压降小于0.06Mpa、分离精度为10um，分离效率不低于80％。
较佳的，所述深度聚结分离模块的体积比表面积为20000～24000m 2/m 3、空隙率为0.71～0.69、模块深度为200～400mm、压降小于0.2Mpa、分离精度为2um，分离效率不低于95％。
较佳的，所述初步聚结分离模块和所述深度聚结分离模块中的金属骨架纤维所使用的材质，当生产水中氯离子含量低于1000mg/L时，所述金属骨架纤维材质可使用316L或904L纤维；当生产水中氯离子含油高于2000mg/L时，所述金属骨架纤维材质必须为钛合金纤维。
本发明的有益效果在于：通过在现有工艺中增加高效深度的聚结除油设备，使得生产水处理工艺和设备能够应对高油含量及高乳化程度下的生产水除油要求，能保证在气田进一步降压生产工况下的生产水达标排放，具有高效、简单和适应性强的特点。
附图说明
图1为实施例1的生产水处理工艺流程示意图；
图2为实施例1的一级油包聚结除油装置的结构示意图；
图3为两级油包聚结除油装置的结构示意图。
符号说明：
11为生产分离器；12为生产水增压泵；13为水力旋流器；14为生产水闪蒸罐；15为凝析油聚结器；16为凝析油闪蒸罐；17为回收油罐；18为回收油传输泵；19固体过滤器；110为聚结除油装置；21、31为入口分布器；22、32为整流器；23、33为初步聚结分离模块；24、37为深度聚结分离模块；25、34、38为强化沉降模块；26、35为一级油包；27、36为界位计接口；39为二级油包。
具体实施方式
下面结合附图和实施例对本发明做进一步说明。
一种海上气田平台生产水处理的方法，包括以下工艺步骤：
步骤(1)：当生产分离器11的出水油含量低于5000mg/L时，聚结除油装置替代生产水增压泵12和水力旋流器13，所述生产分离器的出水直接进入所述聚结除油装置，聚结除油后的净化水进入生产水闪蒸罐14脱气缓冲后排海，聚结除油后的污油排入回收油罐；
步骤(2)：当生产分离器的出水油含量高于5000mg/L时，聚结除油装置串联在水力旋流器之后，所述生产分离器的出水经生产水增压泵进入水力旋流器，旋流除油后的污油排入回收油罐，旋流除油后的生产水进入聚结除油装置110，聚结除油后的净化水进入生产水闪蒸罐，聚结除油后的污油排入回收油罐。
步骤(2)中所述经水力旋流器旋流除油后的生产水中油含量小于1000mg/L。
步骤(1)和步骤(2)所述生产分离器出水为不含或含微量固体颗粒或油泥的液体，若所述生产分离器出水含有大量固体颗粒或油泥，则在所述生产分离器和所述聚结除油装置之间增加10～50um精度的固体过滤器19，所述固体过滤器对50um以上固体颗粒的过滤效率不低于95％；所述聚结除油装置内的聚结模块可以允许小于50um的固体颗粒通过。
步骤(1)和步骤(2)所述聚结除油装置内部支架具有一定压差承受强度，需在聚结除油装置进出口管路上设置压差过载保护，瞬时压差超过1.5MPa时，聚结除油装置出口阀门自动关闭。
一种实现上述任一所述分离方法的聚结除油装置，所述聚结除油装置包括 罐体和油包、入口分布器21、整流器22、初步聚结分离模块23、深度聚结分离模块24、强化沉降模块25；
在一个优选的实施方式中，步骤(1)中所述生产分离器的出水油含量小于2000mg/L，所述聚结除油装置设置一级油包，装置内部生产水延流动方向依次经过入口分布器、整流器、初步聚结分离模块、深度聚结分离模块、强化沉降模块，然后分离后的油进入一级油包排出，分离后的生产水由装置出水口排出；
在另一个优选的实施方式中，步骤(1)中所述生产分离器的出水油含量2000～5000mg/L，所述聚结除油装置设置两级油包，装置内生产水延流动方向依次经过入口分布器、整流器、初步聚结分离模块、强化沉降模块，然后分离出的油进入一级油包26排出，分离后的水再继续流经深度聚结分离模块、强化沉降模块，最后分离出的油进入二级油包39排出，分离出的生产水由装置出水口排出。
较佳的，所述聚结除油装置的一级或二级油包都采用界位-控制阀联动自动控制，间断式排油。
较佳的，所述聚结除油装置内流体截面流速为0.008～0.02m/s，所述初步聚结和所述深度聚结模块内为层流机理。
较佳的，所述初步聚结分离模块的体积比表面积为7000～15000m 2/m 3、空隙率为0.75～0.85、模块深度为200～400mm、压降小于0.06Mpa、分离精度为10um，分离效率不低于80％。
较佳的，所述深度聚结分离模块的体积比表面积为20000～24000m 2/m 3、空隙率为0.71～0.69、模块深度为200～400mm、压降小于0.2Mpa、分离精度为2um，分离效率不低于95％。
较佳的，所述初步聚结分离模块和所述深度聚结分离模块中的金属骨架纤维所使用的材质，当生产水中氯离子含量低于1000mg/L时，所述金属骨架纤维材质可使用316L或904L纤维；当生产水中氯离子含油高于2000mg/L时，所述金属骨架纤维材质必须为钛合金纤维。
实施例1
某海上气田平台的生产水处理工艺中，采用了本发明的升级改造方法及装置，改造后生产水处理工艺流程示意图参阅图1。
改造之前该工艺的运行状态为：处理量15m 3/h；生产水含微量固体颗粒，氯离子含量2000mg/L；生产分离器出水油含量小于1500mg/L、油滴粒径分布范围1～100um、中位粒径12um；水力旋流器分离效率约80％；排海生产水油含量约300mg/L。
方案选择：增加前置固体过滤器；正常运行时聚结除油装置直接替代生产水增压泵12和水力旋流器13；采用一级油包聚结除油装置，装置结构示意图参阅图2；装置内径600mm；初步聚结分离模块23体积比表面积为12000m 2/m 3，模块深度为400mm，金属骨架纤维为钛合金；深度聚结分离模块24体积比表面积为22000m 2/m 3，模块深度为400mm，金属骨架纤维为钛合金；强化沉降模块25深度为200mm；油包26上设置有界位自动控制排油。
实施例1的串联和并联之间的切换说明：
正常并联运行时，全部开启的阀门有：V3、V7，保持控制阀V5自动控制，全部关闭的阀门有：V1、V2、V4、V6。
正常串联运行时，全部开启的阀门有：V1、V4、V7，保持控制阀V5自动控制，全部关闭的阀门有：V2、V3、V6。
采用本发明方法及装置改造后的运行测试效果如下表
Figure PCTCN2018098504-appb-000001
结果分析：经聚结除油装置除油后生产水中油含量能稳定降低至30mg/L以内，保证了生产水达标排放，证明了该改造方法及装置具有良好的应用效果。
综上所述仅为本发明的较佳实施例而已，并非用来限制本发明的实施范围；在阅读了本发明的上述讲述内容之后，本领域技术人员可以对本发明做出的一些非本质的改进和调整，仍属于本发明的保护范围。

Claims (8)

  1. 一种海上气田平台生产水处理方法，其特征在于：在原生产水处理流程的基础上增设聚结除油装置，该装置并联替代原生产水增压泵和水力旋流器，或串联在水力旋流器之后；
    当生产分离器正常工况下，聚结除油装置直接并联替代生产水增压泵和水力旋流器，生产分离器的出水直接进入聚结除油装置，聚结除油后的净化水进入生产水闪蒸罐脱气缓冲后排海，聚结除油后的污油排入回收油罐；
    当生产分离器异常工况下，聚结除油装置串联在水力旋流器之后，生产分离器的出水首先经生产水增压泵进入水力旋流器，旋流除油后的污油排入回收油罐，然后旋流除油后的生产水进入聚结除油装置，聚结除油后的净化水进入生产水闪蒸罐，聚结除油后的污油排入回收油罐；
    所述生产分离器工况正常或异常的判断标准为生产分离器的出水油含量是否高于5000mg/L，当生产分离器出水高于5000mg/L时为异常工况，此时聚结除油装置串联在水力旋流器之后；当生产分离器出水低于5000mg/L时为正常工况；
    所述聚结除油装置在上述工艺流程中的位置为并联替代原生产水增压泵和水力旋流器，或串联在水力旋流器之后；通过管道阀门切换实现并联或串联。
  2. 根据权利要求1所述的方法，其特征在于：当所述生产分离器的出水中固体颗粒或油泥的含量大于10mg/L，则在生产分离器和聚结除油装置之间增加 10～50um精度的固体过滤器，所述固体过滤器对50um以上固体颗粒的分离效率不低于95％。
  3. 根据权利要求1所述的方法，其特征在于：所述聚结除油装置进出口管路上需设置差压计，所述差压计联动控制聚结除油装置出口阀门，对聚结除油装置进行差压过载保护，控制最大瞬时差压不超过1.3～1.5MPa。
  4. 一种海上气田平台生产水处理装置，是一种海上气田平台生产水处理的聚结除油装置，其特征在于：在原生产水处理流程的基础上增设聚结除油装置，该装置并联替代原生产水增压泵和水力旋流器，或串联在水力旋流器之后；
    当聚结除油装置进口生产水油含量小于2000mg/L时，聚结除油装置设置一级油包，装置内生产水延流动方向依次设置有入口分布器、整流器、初步聚结分离模块、深度聚结分离模块、强化沉降模块，然后分离后的油进入一级油包排出，分离后的生产水由装置出水口排出；
    当聚结除油装置进口生产水油含量2000mg/L～5000mg/L时，聚结除油装置设置两级油包，装置内生产水延流动方向依次设置有入口分布器、整流器、初步聚结分离模块、强化沉降模块，然后分离出的油进入一级油包排出，分离后的水再继续流经深度聚结分离模块、强化沉降模块，最后分离出的油进入二级油包排出，分离出的生产水由装置出水口排出。
  5. 根据权利要求4所述的海上气田平台生产水处理装置，其特征在于：聚结除油装置内流体截面流速为0.008～0.02m/s；初步聚结分离模块的分离精度为10um，分离效率不低于80％；深度聚结分离模块的分离精度为2um，分离效率不低于95％。
  6. 根据权利要求4所述的海上气田平台生产水处理装置，其特征在于：初步聚结分离模块的体积比表面积为7000～15000m2/m3、空隙率0.75～0.85、模块深度200～400mm、压降小于0.06Mpa；深度聚结分离模块的体积比表面积为20000～24000m2/m3、空隙率0.69～0.71、模块深度200～400mm、压降小于0.2Mpa。
  7. 根据权利要求4所述的海上气田平台生产水处理装置，其特征在于：当生产水中氯离子含量低于1000mg/L时，初步及深度聚结模块中的骨架纤维材质使用316L纤维；当生产水中氯离子含油高于2000mg/L时，初步及深度聚结模块中的骨架纤维材质为钛合金纤维。
  8. 根据权利要求4所述的海上气田平台生产水处理装置，其特征在于：所述一级或二级油包均采用界位-控制阀联动自动控制，间断式排油。
PCT/CN2018/098504 2017-08-04 2018-08-03 一种海上气田平台生产水处理方法及其装置 Ceased WO2019024915A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201710661499.4 2017-08-04
CN201710661499.4A CN107381914A (zh) 2017-08-04 2017-08-04 一种海上气田平台生产水处理方法及其装置

Publications (1)

Publication Number Publication Date
WO2019024915A1 true WO2019024915A1 (zh) 2019-02-07

Family

ID=60343836

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2018/098504 Ceased WO2019024915A1 (zh) 2017-08-04 2018-08-03 一种海上气田平台生产水处理方法及其装置

Country Status (2)

Country Link
CN (2) CN110759566B (zh)
WO (1) WO2019024915A1 (zh)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114455670A (zh) * 2022-01-18 2022-05-10 华东理工大学 一种炼油污水异性介质组合除油除悬系统及方法
CN114477369A (zh) * 2022-01-18 2022-05-13 华东理工大学 一种脱气及轻重油同步分离的酚氨废水预处理装置和工艺
CN114524482A (zh) * 2022-01-18 2022-05-24 华东理工大学 一种乙丙烷脱氢装置工艺水除油脱固一体化装置及方法
CN114538639A (zh) * 2022-01-18 2022-05-27 华东理工大学 一种含油污水进生化前的预处理系统及方法
CN114958410A (zh) * 2021-02-24 2022-08-30 中国石油天然气集团有限公司 一种处理高含水稠油的撬装电脱水系统和方法
CN115385451A (zh) * 2022-08-15 2022-11-25 宇星环保工程有限公司 一种两级a/o活性污泥法污水处理系统及工艺

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110759566B (zh) * 2017-08-04 2022-11-11 华东理工大学 一种海上气田平台生产水处理方法
CN109179930B (zh) * 2018-09-30 2020-12-01 华东理工大学 一种罐底油泥中油、泥、水三相分离以及油泥中油的高效回收的方法
CN109502786A (zh) * 2018-11-30 2019-03-22 中石化石油工程技术服务有限公司 油类污水处理系统
CN110078236A (zh) * 2019-04-15 2019-08-02 华东理工大学 一种适用于海上油田平台的水处理系统及其处理方法
CN110143735A (zh) * 2019-06-30 2019-08-20 天津泰兴工程技术有限公司 一种高效净化处理不同物性油泥砂的方法及装置
CN111686950B (zh) * 2020-06-11 2022-01-07 中科合成油技术股份有限公司 一种高温高压下油水快速分离的方法及装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0273463A1 (en) * 1987-01-02 1988-07-06 Arfaz Equipment Method for cleaning oilfield product storage tanks
CN2504256Y (zh) * 2001-03-04 2002-08-07 北京华油惠博普科技有限公司 组合式除油器
CN101638274A (zh) * 2009-09-03 2010-02-03 江苏新龙鼎环保成套工程有限公司 移动式采油井洗井含油废水处理成套装置
CN102826703A (zh) * 2012-09-17 2012-12-19 曹式芳 蒸汽凝结水回收及除油去离子净化处理系统
CN107381914A (zh) * 2017-08-04 2017-11-24 华东理工大学 一种海上气田平台生产水处理方法及其装置

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2107947B1 (en) * 2007-01-09 2016-03-16 Evoqua Water Technologies LLC A system and method for removing dissolved contaminants, particulate contaminants, and oil contaminants from industrial waste water
CN101070199B (zh) * 2007-03-22 2010-12-15 华东理工大学 含油污水的油相富集方法及装置
CN102745771B (zh) * 2012-02-21 2015-03-04 胜利油田胜利勘察设计研究院有限公司 多相流装配式密闭聚结除油装置
CN204079541U (zh) * 2014-05-19 2015-01-07 华东理工大学 一种对含低浓度污油的废水进行深度除油的装置
CN104773789B (zh) * 2015-04-08 2016-08-24 华东理工大学 一种紧凑型三相分离方法及装置

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0273463A1 (en) * 1987-01-02 1988-07-06 Arfaz Equipment Method for cleaning oilfield product storage tanks
CN2504256Y (zh) * 2001-03-04 2002-08-07 北京华油惠博普科技有限公司 组合式除油器
CN101638274A (zh) * 2009-09-03 2010-02-03 江苏新龙鼎环保成套工程有限公司 移动式采油井洗井含油废水处理成套装置
CN102826703A (zh) * 2012-09-17 2012-12-19 曹式芳 蒸汽凝结水回收及除油去离子净化处理系统
CN107381914A (zh) * 2017-08-04 2017-11-24 华东理工大学 一种海上气田平台生产水处理方法及其装置

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114958410A (zh) * 2021-02-24 2022-08-30 中国石油天然气集团有限公司 一种处理高含水稠油的撬装电脱水系统和方法
CN114958410B (zh) * 2021-02-24 2024-05-28 中国石油天然气集团有限公司 一种处理高含水稠油的撬装电脱水系统和方法
CN114455670A (zh) * 2022-01-18 2022-05-10 华东理工大学 一种炼油污水异性介质组合除油除悬系统及方法
CN114477369A (zh) * 2022-01-18 2022-05-13 华东理工大学 一种脱气及轻重油同步分离的酚氨废水预处理装置和工艺
CN114524482A (zh) * 2022-01-18 2022-05-24 华东理工大学 一种乙丙烷脱氢装置工艺水除油脱固一体化装置及方法
CN114538639A (zh) * 2022-01-18 2022-05-27 华东理工大学 一种含油污水进生化前的预处理系统及方法
CN114524482B (zh) * 2022-01-18 2023-12-05 华东理工大学 一种乙丙烷脱氢装置工艺水除油脱固一体化装置及方法
CN114538639B (zh) * 2022-01-18 2024-01-26 华东理工大学 一种含油污水进生化前的预处理系统及方法
CN114455670B (zh) * 2022-01-18 2024-01-26 华东理工大学 一种炼油污水异性介质组合除油除悬系统及方法
CN115385451A (zh) * 2022-08-15 2022-11-25 宇星环保工程有限公司 一种两级a/o活性污泥法污水处理系统及工艺

Also Published As

Publication number Publication date
CN110759566B (zh) 2022-11-11
CN110759566A (zh) 2020-02-07
CN107381914A (zh) 2017-11-24

Similar Documents

Publication Publication Date Title
WO2019024915A1 (zh) 一种海上气田平台生产水处理方法及其装置
RU2618783C2 (ru) Система сепарации мультифазного потока
CN1681572A (zh) 用于分离多相流体的装置
CN105621517A (zh) 基于单罐双级旋流气浮装置进行含油污水处理的装置和方法
CN103408153A (zh) 含乳化油污水物理破乳处理装置及其处理方法
CN116354438A (zh) 一种基于立式浅层气浮的含气油田采出水处理装置及方法
CN114164020A (zh) 海上油田原油脱水处理系统及工艺
CN103883305B (zh) 一种深水海底油水分离及回注装置
CN107352668A (zh) 一种基于水合物法的油田伴生气回收和采出污水处理装置
CN102989200B (zh) 一种溢油回收机器人用油水分离工艺及设备
CN111686950B (zh) 一种高温高压下油水快速分离的方法及装置
WO2020211734A1 (zh) 一种适用于海上油田平台的水处理系统及其处理方法
WO2020001246A1 (zh) 一种酸性水脱气除油方法及其装置
CN101070199B (zh) 含油污水的油相富集方法及装置
CN113482586A (zh) 一种海上热采稠油集输处理工艺包
RU2045982C1 (ru) Установка подготовки продукции скважин
CN107557058B (zh) 一种紧凑型组合闪蒸原油脱气方法和装置
CN104528988A (zh) 一种气田含油含醇污水预处理系统及其方法
CN105000704B (zh) 管道式油气水分离器及分离方法
CN115477412A (zh) 一种海上平台生产水处理方法
CN104629794B (zh) 一种耦合油气洗涤的油水初步分离方法及装置
CN216008468U (zh) 海上热采稠油集输处理工艺包
CN110510798A (zh) 一种用微气泡深度处理三元复合驱采出水的方法
CN118145739B (zh) 一种超空化气浮油水分离装置及分离方法
CN113307399A (zh) 一种海上油田高含油生产水分级净化的装置和方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18840654

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 18840654

Country of ref document: EP

Kind code of ref document: A1