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WO2016127273A1 - 一种强化冷低压分离器中油水分离及耦合除盐功能的方法及装置 - Google Patents

一种强化冷低压分离器中油水分离及耦合除盐功能的方法及装置 Download PDF

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Publication number
WO2016127273A1
WO2016127273A1 PCT/CN2015/000302 CN2015000302W WO2016127273A1 WO 2016127273 A1 WO2016127273 A1 WO 2016127273A1 CN 2015000302 W CN2015000302 W CN 2015000302W WO 2016127273 A1 WO2016127273 A1 WO 2016127273A1
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Prior art keywords
water
oil
separation
module
gas
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English (en)
French (fr)
Inventor
杨强
卢浩
刘森
王朝阳
许萧
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East China University of Science and Technology
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East China University of Science and Technology
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Priority to US15/549,385 priority Critical patent/US20180023009A1/en
Priority to EP15881435.0A priority patent/EP3257565B1/en
Publication of WO2016127273A1 publication Critical patent/WO2016127273A1/zh
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    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • 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
    • 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
    • B01D17/0208—Separation of non-miscible liquids by sedimentation
    • B01D17/0214—Separation of non-miscible liquids by sedimentation with removal of one of the phases
    • 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
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/045—Breaking emulsions with coalescers
    • 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
    • B01D17/04—Breaking emulsions
    • B01D17/047—Breaking emulsions with separation aids
    • 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
    • B01D17/12—Auxiliary equipment particularly adapted for use with liquid-separating apparatus, e.g. control circuits
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • 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
    • 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
    • C10G2300/205—Metal content
    • 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
    • C10G2300/80—Additives
    • C10G2300/805—Water

Definitions

  • the invention relates to the field of petroleum refining or coal chemical industry, and relates to a method and a device for strengthening oil-water separation and coupling de-salting function in a cold low-pressure separator.
  • the working principle of the low pressure separator belongs to the equilibrium vaporization in the distillation operation, that is, the feed is in a certain way, after decompression, in a space of a container, under a certain temperature and pressure, steam, The two phases of the liquid are separated immediately, and the corresponding gas phase and liquid phase products are obtained.
  • the function of the low-pressure separator is to separate the gas-liquid component in the incoming material of the cold high-pressure separator, flash off part of the gas phase component, and reduce the gas phase load of the fractionation system; second, because the gas phase component contains more sulfurization. Hydrogen, after removing a portion of the hydrogen sulfide in the low pressure separator, reduces equipment corrosion in the fractionation system.
  • the low-pressure separator is separated by a conventional gravity sedimentation tank.
  • the current design does not consider the desalination function of the low pressure separator. Therefore, new low-efficiency separators need to be optimized with new and efficient technologies.
  • the present invention provides a method and a device for enhancing oil-water separation and coupling de-salting function in a cold low-pressure separator, which combines material properties and flow field control to carry out enhanced separation of oil and water, and simultaneously adopts a water-washing method.
  • the hydrogen sulfide and salts entrained in the oil are washed and removed, and the separation of oil and water is enhanced, and the purpose of high-efficiency demineralization is achieved, which makes up for the shortcomings of the existing cold low-pressure separator technology.
  • a method for enhancing oil-water separation and coupling de-salting in a cold low-pressure separator comprising the following steps:
  • Step 1 The aqueous low-oil is mixed with the desalted water in the inlet section. During this process, the salt and hydrogen sulfide in the mixture are transferred to the water, and the initial salt washing is carried out to enter the T-type liquid gas separator, and the low-separation oil is quickly separated. Pressure a low-gas separation flashed; wherein the aqueous low-alloy oil has a pressure in the inlet section of 0.6 to 4.5 MPa, a temperature of 20 to 90 ° C, and a volume percentage of the demineralized water injection amount of 0 to 1%;
  • Step 2 The oil-water mixture is washed and rectified by secondary water injection and then enters the preliminary separation section.
  • the hydrophilic water droplet coarse granulation module is used to rapidly coalesce and disperse the water droplets in the oil, and then the CPI rapid separation module realizes rapid separation of oil and water.
  • the water is automatically discharged from the bottom through the oil-water boundary controller or through the left and right communication ports of the partition plate into the deep separation chamber, and the oil and trace water are processed through the partition plate in the next step; wherein the volume percentage of the secondary water injection amount is 0 ⁇ 0.5%, the flow velocity of the oil-water mixture after rectification distribution is 0.005 ⁇ 0.05m/s, and the corrugated plate spacing of the CPI module is 5 ⁇ 18mm, in this process, water droplets with particle diameter greater than 30 ⁇ m are separated;
  • Step 3 After the oil and trace water enter the deep separation section, the water droplets with larger particle size are first separated into the water bag by gravity sedimentation, and then deepened by a combined fiber dehydration module including hydrophilic fibers and lipophilic fibers. Dehydration, this process realizes the separation of water droplets with a particle size of 3 ⁇ 30 ⁇ m entrained in the oil; the oil after deep dehydration is automatically controlled and discharged by the liquid level controller, and the separated water enters the combined fiber including hydrophilic fibers and lipophilic fibers.
  • the oil and water interface controller automatically controls the outer row, and the process is separated by the combined fiber module to reach an oil content of less than 100 mg/L;
  • the ratio of the hydrophilic fibers to the lipophilic fibers in the combined fiber dewatering module is 5 to 15%; and the ratio of the lipophilic fibers to the hydrophilic fibers in the combined fiber degreasing module is 10 to 20%.
  • the injection method of the desalted water in step 1 is countercurrent or downstream, and the diameter of the injected water droplets is 10 to 50 ⁇ m, and the injection amount can be adjusted according to the salt content in the oil.
  • the flow rate of the mixed liquid in the inlet section of the T-type liquid gas separator described in the step 1 is 3 to 6 m/s.
  • the method of the second water injection in the step 2 is that the water is injected countercurrently through the inner tube and the nozzle, and the water droplet diameter of the water injection is 30 to 100 ⁇ m.
  • the hydrophilic water droplet coarse granulation module and the CPI rapid separation module according to step 2 are modified Teflon, polypropylene or stainless steel materials.
  • the composite fiber module in the step 3 is in the form of weaving in Chinese Patent Publication No. 103952853A.
  • An apparatus for realizing oil-water separation and coupling demineralization function in a reinforced cold low-pressure separator comprising a casing, an oil-water gas inlet disposed on the casing, and the oil-water
  • the water inlet device connected with the gas inlet and the T-type liquid gas separator or the cyclone degasser are respectively arranged in the secondary water injector, the rectifying distributor, the oil and water coarse granulation module, the CPI rapid separation module, the oil water inside the casing.
  • Boundary a surface controller, a separator, a level controller, and an oil phase outlet at a tail of the housing; a gas eliminator disposed at a bottom of the housing, the top of the housing having a gas phase outlet; the housing There is also a water phase outlet at the bottom.
  • the oil phase outlet, the gas phase outlet and the water phase outlet are respectively provided with regulating valves;
  • the gas liquid trap has an oil-water interface controller inside.
  • the housing is horizontal or vertical.
  • the invention adopts the T-type liquid-gas separation technology, on the one hand, the depressurized flash gas realizes rapid liquid degassing by the centrifugal force of the T-tube liquid rotating, the structure is simple and the separation efficiency is higher than the gravity sedimentation separation;
  • the inlet flow rate of the T-tube is controlled to 3 to 6 m/s, the uniformly dispersed water droplets are subjected to the centrifugal force of rotation in the T-tube, and the water droplets are in the radial direction due to the difference in oil-water density.
  • the cross-section is the movement from the inside to the outside, and the vertical section is from the top to the bottom, which can complete the secondary washing and desalting function, and the water droplets with the particle size of 10 ⁇ 50 ⁇ m are not easy to be broken and emulsified under the centrifugal force, and the subsequent high-efficiency separation is satisfied;
  • a water film is formed on the surface of the baffle plate of the coarse granulation module, and small water droplets entrained in the oil, such as water droplets smaller than 30 ⁇ m, can quickly combine with the water film to form large droplets, thereby improving the coalescence performance of the coarse granulated water droplets;
  • the coarse dehydration separation and the fine dehydration separation are realized in one shell, and the water droplets larger than 30 ⁇ m are mainly removed before the separator, and the composite fiber is used to realize the deep dehydration function after the separator, and the hydrophilic fiber in the dehydration module
  • the proportion of oleophilic fiber is 5-15%, and the deep separation of water droplets is achieved while maintaining the low pressure drop (the oil easily passes through the fiber layer through the oleophilic fiber) (partially emulsified oil droplets entrain tiny water droplets, and this part of the water droplets are pro- Water-based fiber interception and separation), through this step-by-step classification method, the effect of deep dewatering in oil can be achieved. More importantly, the oil dehydration separation time is reduced from the current design of 10 minutes to less than 3 minutes. Fast, high efficiency and greatly reduced equipment, and system supporting costs are also reduced;
  • the water injection port can be closed, and the water is distributed from the left side of the partition to the water bag by using the joint port on the left and right sides of the partition plate.
  • the design of the partition plate is beneficial to realize the preliminary separation and stratification of oil and water. , reducing the fluctuation of water in the low oil split and causing the oil content of the low oil outlet to increase.
  • the device used in the invention has the characteristics of small occupied area, high speed of separation of oil and water, high efficiency, enhanced function of degassing and dehydration of the prior art, and increased demineralization function, and can be widely applied to petroleum refining.
  • the low-separation separation process of the process can also be applied to a separation process such as an overhead reflux tank.
  • FIG. 1 is a view showing the apparatus for oil-water separation and coupling desalination in a reinforced cold low-pressure separator of the first embodiment.
  • the oil-water separation and coupling de-salting function device in the reinforced cold low-pressure separator comprises a casing, an oil-water inlet 1 disposed on the casing, and a water injection port 2-1 connected to the oil-water inlet 1 respectively.
  • T-type liquid-gas separator 3 (or cyclone degasser), secondary water injector (including water injection port 2-2), rectifying distributor 4, oil-water coarse granulation module 5, CPI fast a separation module 6, (oil-water) interface controllers 13-1, 13-2, a partition 18, a level controller 10, and an oil phase outlet 19 at the rear of the housing; a deep degreasing module 7 disposed at the bottom of the housing,
  • the top of the housing has a gas phase outlet 8; the bottom of the housing is also provided with a water phase outlet 17.
  • the oil phase outlet 10, the water phase outlet 17, and the water phase outlet 16 are respectively provided with a regulating valve 11-1, 11-2, 11-3.
  • the housing can be horizontal or vertical.
  • Example 1 was horizontal.
  • the low-separation oil enters from the oil-water inlet 1 and a part of the gas is flashed out due to the effect of the pressure reduction.
  • the oil-water gas is injected into the water-filling port 2-1 with a particle size of 10 to 50 ⁇ m, and the salt water is mixed for countercurrent contact to complete the preliminary salt washing.
  • the function then enters the T-type liquid-gas separator for rapid separation of the liquid gas. Since the T-type liquid-gas separator completes the rapid separation of the liquid gas by the centrifugal force of rotation by the tangential inlet, the injection port is injected while rotating and separating.
  • the water droplets gradually move outward in the radial section of the T-type separator under the action of centrifugal force, and move downward in the axial section to complete the secondary salt washing process.
  • the oil-water mixture enters the low-pressure separation from the lower outlet of the T-type separator. Device.
  • the oil-water mixture flows from left to right, and is first mixed and washed with 30-50 ⁇ m desalted water injected into the water inlet 2-2, during which the deep washing is completed, and then the rectifying distributor 4 is introduced to perform rectification distribution of the fluid to realize oil water.
  • the mixture is uniformly distributed in the diameter section of the vessel, and the flow velocity of the oil-water mixture after the rectification distribution is 0.005 to 0.05 m/s; secondly, the oil-water mixture enters the oil-water coarse granulation module 5 to flow up and down between the coarse-grained baffles, Due to the hydrophilicity of the surface of the coarse-grained baffle, the large-particle water droplets in the oil-water mixture rapidly form a water film on the surface of the plate to further adsorb the small-sized water droplets in the oil, causing it to coalesce and grow, and the oil water passes through the process.
  • the mixture enters the CPI rapid separation module 6, and relies on the shallow pool sedimentation principle of the multi-layer corrugated board to quickly complete the preliminary oil dehydration process, which can effectively separate water droplets larger than 30 ⁇ m in particle size, and the oil-water interface forms an oil-water interface on the left side of the separator 18.
  • the interface controller 13-2 the opening of the regulating valve 11-3 is controlled, and the water phase outlet 16 is introduced into the water phase mixing outlet 12 to complete the water discharge, and the oil passes through the partition plate 18. Enter the deep dehydration process.
  • the particle size of the water droplets entering the deep dewatering zone is generally less than 30 ⁇ m.
  • a natural sedimentation zone is set on the right side of the partition plate, and some settled water droplets are settled and separated into the bottom of the tank to enter the water bag.
  • this section can be buffer adjusted; after that, the oil-water mixture containing fine water droplets enters the deep dewatering module 9, and the hydrophilic fiber in the deep dewatering module 9 accounts for 5 to 15% of the lipophilic fiber, keeping the low pressure drop.
  • the oil easily passes through the fiber layer through the oleophilic fiber) to achieve deep separation of the water droplets (partially emulsified oil droplets entrain tiny water droplets, and this part of the water droplets are intercepted by hydrophilic fibers); the water droplets intercepted pass through the hydrophilic fibers
  • the coalescing action is settled into the water bag, and then the oil removal process is performed by the deep degreasing module 7 composed of the combined fibers, and the oil-water interface layer is formed in the water bag by the natural sedimentation method, and the regulating valve 11 is controlled by the boundary controller 13-1. -2 opening, from the water phase outlet 17 into the water phase mixing outlet 12 The efflux of the water is completed; the oil is discharged from the oil phase outlet 19 by the liquid level controller 10 to control the regulating valve 11-1.
  • the communication valve 14 is opened, and the water enters the water bag for efflux.
  • Table 1 shows the properties and operating parameters of a cold low pressure separator for a refinery hydrogenation unit.
  • the original cold low pressure separator is designed as a gravity sedimentation tank with a diameter of 2000mm and a tangent length of 5800mm for three-phase separation of oil and water.
  • the water content in the oil phase outlet often exceeds 2000ppm, and the water phase is exported.
  • the medium water has more than 1000ppm of oil, and there is a problem that the stripping tower and the fractionation tower after the cold low pressure separator are severely corroded, which brings problems to the long cycle and economic operation of the device. Therefore, the process is modified by the technique of the present invention:
  • the water content in the export oil is less than 300ppm, the oil content in the water is less than 200ppm, eliminating the salt corrosion of the stripping and fractionation tower after the cold and low pressure separation, and ensuring long-term operation.
  • Process parameters Calculated according to the liquid flow rate of 0.02m/s, the average liquid level height is 50%, and the residence time is 180s.
  • the diameter of the equipment after the transformation is 1600mm, the length of the tangent is 3600mm;
  • the amount of corrosion was found after half a year of operation, so it was designed to be filled once, and the amount of water injected was 0.5% of the flow rate of the oil phase.
  • the inlet adopts T-type liquid-gas separator, the inlet flow rate is controlled to 4.8m/s, which meets the requirement of oil-water mixed separation while achieving liquid degassing;
  • the water droplet coarse granulation module 5 adopts 316L stainless steel baffle
  • the board is coarsely granulated, and the CPI module adopts modified PP corrugated board.
  • the board spacing is controlled to 10mm, the recessed opening ratio is 3%, which meets the rapid settlement after the water droplets coalesce;
  • the deep dewatering module 7 uses nylon and Teflon.
  • the mass ratio of the three is 2:7:1;
  • the deep degreasing module 7 is a mixture of glass fiber, Teflon fiber and 316L stainless steel fiber, of which the mass ratio of the three is 6 : 3:1.
  • the hydrogen content in the oil in the cold low pressure separator is reduced by 22%
  • the oil content in the outlet water is 80-180 ppm
  • the water content in the outlet oil is 210-290 ppm
  • the chloride ion content is reduced to 11 ⁇ g. /g, compared with the original gravity sedimentation separation process technology, the following beneficial effects:

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Abstract

一种强化冷低压分离器中油水分离和耦合除盐的方法及其装置，含水低分油在入口段与体积比为0～1％的脱盐水逆流混合后进入T型液气分离器（3）进行脱气处理，将气相快速分离，油水混合物在低压分离器下部自左封头向右流动至整流分布器（4）实现在径向截面的均布；油水依次通过油水粗粒化模块（5）及CPI快速分离模块（6）分离后一部分水外排，油及微量水(0～0.01％)通过隔板（18）后进入深度分离段，油通过纤维组合模块深度脱水后外排，拦截下的水通过纤维组合模块深度除油后外排。

Description

一种强化冷低压分离器中油水分离及耦合除盐功能的方法及装置 技术领域
本发明涉及石油炼制或者煤化工领域，涉及一种强化冷低压分离器中油水分离及耦合除盐功能的方法及装置。
背景技术
在加氢装置中，低压分离器的工作原理属于蒸馏操作中的平衡汽化，即进料以某种方式，经过减压后，在一个容器的空间内，在一定的温度、压力下，汽、液两相迅即分离，得到相应的气相和液相产物。低压分离器作用一是将冷高压分离器来料中的气液相组分进行分离，闪蒸出部分气相组分，降低分馏系统的气相负荷；二是因为气相组分中含有较多的硫化氢，在低压分离器中脱除一部分硫化氢后，会减少分馏系统的设备腐蚀。
目前低压分离器采用常规的重力沉降罐进行分离，在运行过程中存在以下三点问题：(1)液气分离效果较差，因为降压闪蒸分离出的分散的微小气泡靠重力沉降无法有效去除，被夹带进入酸性水或者馏分油中，造成气体资源流失(主要为氢气)，另外也会增大下游负荷；(2)油水采用重力沉降分离，设计停留时间为10分钟或者更长，分离效果差且占地面积大；(3)油品质量变差后，馏分油中含盐含硫化氢量增大，馏分油脱水效果差，水中含硫化氢及盐类导致下游汽提及分馏过程腐蚀严重，当前设计未考虑低压分离器的除盐功能。因此需采用新型高效的技术对当前低压分离器进行优化。
发明内容
鉴于上述问题，本发明提供一种强化冷低压分离器中油水分离及耦合除盐功能的方法及装置，其结合材料特性及流场调控两方面进行油水的强化分离，并同时采用注水洗涤方式对油中夹带的硫化氢及盐类进行洗涤脱除，再强化油水分离的同时且达到高效除盐的目的，弥补了现有冷低压分离器技术的不足。
具体的技术方案为：
一种强化冷低压分离器中油水分离和耦合除盐的方法，包括以下步骤：
步骤1：含水低分油在入口段与脱盐水混合，在此过程混合物中的盐及硫化氢转移到水中，完成初步洗盐后进入T型液气分离器，快速分离低分油中因降压 闪蒸出的低分气；其中，所述含水低分油在入口段的压力为0.6～4.5MPa，温度为20～90℃，所述脱盐水的注入量的体积百分比为0～1％；
步骤2：油水混合物通过二次注水洗涤及整流分布后进入初步分离段，采用亲水性水滴粗粒化模块将油中分散的水滴快速聚结长大，再通过CPI快速分离模块实现油水快速分离，水从底部通过油水界位控制器自动排出或通过隔板左右的连通口进入深度分离腔，油及微量水通过隔板进下个步骤处理；其中，二次注水量的体积百分含量为0～0.5％，整流分布后油水混合物的流动速度为0.005～0.05m/s，CPI模块的波纹板间距为5～18mm，此过程分离出粒径大于30μm的水滴；
步骤3：油及微量水进入深度分离段后，首先通过重力沉降的方法将粒径较大的水滴分离到底部进入水包，然后通过包括亲水性纤维和亲油性纤维的组合纤维脱水模块进行深度脱水，此过程实现油中夹带的粒径为3～30μm的水滴分离；深度脱水后的油通过液面控制器自动控制排出，分离出的水进入包括亲水性纤维和亲油性纤维的组合纤维除油模块进行除油处理后通过油水界面控制器自动控制外排，此过程经组合纤维模块分离后达到水中含油量小于100mg/L；
其中，所述组合纤维脱水模块中亲水性纤维占亲油性纤维的比例为5～15％；所述组合纤维除油模块中亲油性纤维占亲水性纤维的比例为10～20％。
步骤1所述脱盐水的注入方式为逆流或顺流，注入的水滴粒径为10～50μm，注入量可根据油中含盐量进行调整。
步骤1所述的T型液气分离器入口段的混合液流速为3～6m/s。
步骤2所述二次注水的方式为通过内伸管加喷头逆流注水，注水的水滴粒径为30～100μm。
步骤2所述的亲水性水滴粗粒化模块和所述CPI快速分离模块采用改性的特氟龙、聚丙烯或者不锈钢材料。
步骤3中的组合纤维模块采用中国专利公开号为103952853A中的编织形式。
一种实现上述任一所述方法的强化冷低压分离器中油水分离和耦合除盐功能的装置，所述装置包括壳体、设置在所述壳体上的油水气进口，分别与所述油水气进口相连的注水设备和T型液气分离器或旋流脱气器，依次设置于所述壳体内部的二次注水器、整流分布器、油水粗粒化模块、CPI快速分离模块、油水界 面控制器、隔板、液面控制器以及处于所述壳体尾部的油相出口；置于所述壳体底部的气体脱液器，所述壳体的顶部具有气相出口；所述壳体的底部还设有水相出口。
所述油相出口、气相出口、水相出口上分别设有调节阀；
所述气体脱液器内部具有油水界面控制器。
所述壳体为卧式或立式。
本发明的有益效果在于：
(1)本发明采用T型液气分离技术，一方面降压闪蒸的气体通过T型管液体旋转的离心力实现快速的液体脱气，结构简单且分离效率高于重力沉降分离；另一方面，在T型分离器的前段注水，控制T型管入口流速为3～6m/s时，均匀分散的水滴在T型管中受到旋转离心力的作用，由于油水密度差的原因，水滴在径向截面上是自内向外迁移运动，在垂直截面是自上向下运动，能完成二次洗涤除盐的作用且粒径为10～50μm水滴在此离心力下不易破碎乳化，满足后续的高效分离；
(2)采用二次注水，一方面可以节省注水量，实现深度除盐，另一方面可以提高油水的快速分离，主要原因是一次注水会存在偏流，T型管分离过程停留时间段，导致部分油未与水充分洗涤，因此二次注水可以再次洗盐；其次二次注水控制水的液滴粒径为30～100μm，属于分散态水滴，在粗粒化模块，此部分水滴可以迅速富集到粗粒化模块的折流板表面形成水膜，油中夹带的小水滴，如小于30μm的小水滴可以迅速与水膜结合形成大液滴，提高粗粒化的水滴聚结性能；
(3)一个壳体中实现了粗脱水分离与精细脱水分离，在隔板前主要脱除大于30μm的水滴，再隔板后采用组合纤维实现深度脱水的功能，而脱水模块中亲水性纤维占亲油性纤维比例为5～15％，在保持低压降(油易通过亲油纤维穿过纤维层)而实现水滴的深度分离(部分乳化态油滴会夹带微小水滴，而此部分水滴被亲水性纤维拦截分离)，通过此种分步分级的方法可实现油中深度脱水的作用，更为重要的是通过此设计油脱水分离时间由当前设计的10分钟以上降低到3分钟以内，速度快、效率高且占设备大大减小，系统配套费用也降低；
(4)脱气、注水洗盐、油水强化分离三个技术相互促进提升各自的性能，脱气过程的旋转流动实现脱气同时实现洗盐及油水的粗分离，二次注水在强化洗 盐的同时又由于大粒径的水滴吸水作用可提升油水分离性能，油水错流流动快速分离过程也对洗盐分离有一定的促进作用，因为该发明将以上三种技术进行了耦合设计，满足功能的同时强化了性能；
(5)对于含盐较低的低分油，可以关闭注水口，采用隔板左右的联通口实现水由隔板左侧流通到水包，隔板的设计有利于实现油水的初步分离分层，减小低分油中带水的波动而导致低分油出口含油量增大。
本发明采用的设备具有占地面积小、油水分离速度快效率高的特点，在功能上强化了既有技术的脱气、脱水性能的同时还增加了除盐功能，可广泛应用于石油炼制过程的低分分离流程也可以应用与塔顶回流罐等分离过程。
附图说明
图1是实施例1的具有强化冷低压分离器中油水分离及耦合除盐功能的装置。
符号说明
1 油水气入口；2-1、2-2 注水口；3 T型液气分离器；4 整流分布器；
5 油水粗粒化模块；6 CPI快速分离模块；7 深度除油模块；
8 气相出口；9 深度脱水模块；10 液面控制器；11-1、11-2、11-3 调节阀；
12 水相混合出口；13-1、13-2 界位控制器；14 联通阀；15 水相返回口；
16 水相出口1；17 水相出口2；18 隔板；19 油相出口。
具体实施方式
以下通过实施例对本发明的方法及其装置进行具体描述，但实施例只用于对本发明进一步说明，并不限制本发明的保护范围。
实施例1
如图1所示，该强化冷低压分离器中油水分离及耦合除盐功能装置包括壳体、设置在壳体上的油水气入口1，分别与油水气入口1相连的注水口2-1和T型液气分离器3(或旋流脱气器)，依次设置于壳体内部的二次注水器(含注水口2-2)、整流分布器4、油水粗粒化模块5、CPI快速分离模块6、(油水)界面控制器13-1、13-2、隔板18、液面控制器10以及处于壳体尾部的油相出口19；置于壳体底部的深度除油模块7，壳体的顶部具有气相出口8；壳体的底部还设有水相出口17。油相出口10、水相出口17、水相出口16上分别设有调节阀11-1、 11-2、11-3。
壳体可以为卧式或立式。实施例1采用卧式。
低分油从油水气入口1进入，由于降压的作用会闪蒸出来一部分气体，油水气与注水口2-1注入的粒径为10～50μm脱盐水进行逆流接触混合，完成初步的洗盐作用，接着进入T型液气分离器进行液气的快速分离，由于T型液气分离器是通过切向进口实现的旋转离心力完成液气的快速分离，因此在旋转分离的同时，注水口注入的水滴在离心力作用下在T型分离器的径向截面上逐渐向外运动，在轴向截面上向下运动，完成二次洗盐过程，油水混合物从T型分离器的下部出口进入低压分离器。
油水混合物自左向右流动，首先与注水口2-2注入的30～50μm脱盐水进行在此混合洗涤，在此期间完成深度洗盐，之后进去整流分布器4进行流体的整流分布，实现油水混合物在容器直径截面的均匀分布，整流分布后油水混合物的流动速度为0.005～0.05m/s；其次油水混合物进入油水粗粒化模块5在粗粒化折流板之间进行上下错流流动，由于粗粒化折流板表面的亲水性，油水混合物中的大颗粒水滴迅速在板表面形成水膜进一步吸附油中的小粒径的水滴，使之聚结长大，通过此过程后油水混合物进入CPI快速分离模块6，依靠多层波纹板浅池沉降原理，迅速完成初步的油脱水过程，此过程能将大于30μm粒径的水滴进行有效分离，油水在隔板18左侧形成油水界面，依靠界面控制器13-2控制调节阀11-3的开启，从水相出口16进入水相混合出口12完成水的外排，油则通过隔板18进入深度脱水过程。
进入深度脱水区的水滴粒径一般都小于30μm，首先在隔板右侧设置一段自然沉降区，将部分可沉降的小水滴沉降分离到罐底进入水包，另外，即使上个过程油水分离波动或者入口带水波动，此段能进行缓冲调节；之后含微细水滴的油水混合物进入深度脱水模块9，深度脱水模块9中亲水性纤维占亲油性纤维比例为5～15％，在保持低压降(油易通过亲油纤维穿过纤维层)而实现水滴的深度分离(部分乳化态油滴会夹带微小水滴，而此部分水滴被亲水性纤维拦截分离)；拦截下的水滴通过亲水纤维的聚结作用沉降进入水包，再通过组合纤维构成的深度除油模块7进行除油处理后通过自然沉降方式在水包中形成油水界面层，通过界位控制器13-1控制调节阀11-2的开启，从水相出口17进入水相混合出口12 完成水的外排；油则通过液面控制器10控制调节阀11-1从油相出口19完成油相外排。
进一步，如果油中含盐较低，不需要注水洗盐或者注水量小于0.5％，则开启联通阀14，水进入水包进行外排。
表1为某炼油厂加氢装置冷低压分离器的性质及操作参数。
表1
项目 工艺操作数据
物料名称 油气、油、H2S、氢气、水
总流量 37000kg/h
气相 2703kg/h
油相 34184kg/h
水相 113kg/h
温度 50℃
操作压力 3.0MPa
气相密度 22.835kg/m3
油相密度 685.992kg/m3
氯离子含量 80μg/g
液相中H2S含量 0.6253％(W)
液相中氢浓度 氢浓度0.0236％(W)
依照上述操作参数，原冷低压分离器设计为直径2000mm，切线长度5800mm的一个重力沉降罐进行油水气的三相分离，经过运行半年时间，发现油相出口中水含量经常超过2000ppm，水相出口中水中带油超过1000ppm，且存在经冷低压分离器后的汽提塔、分馏塔腐蚀较严重的问题，对装置的长周期、经济性运行带来了问题。因此采用本发明技术对该过程进行改造：
改造总体要求：出口油中含水量小于300ppm，水中含油量小于200ppm，消除经冷低压分离后的汽提、分馏塔的结盐腐蚀，保障长周期运转。
改造工艺计算如下：
(1)工艺参数：按照液体流速0.02m/s计算，平均液位高度50％，停留时间180s计算，得出改造后设备直径为1600mm，切线长度3600mm；因盐含量为微 量，运行半年后发现腐蚀，因此设计为1次注水，注水量为油相流量的0.5％。
(2)内构件形式：入口采用T型液气分离器，入口流速控制为4.8m/s，在实现液体脱气的同时满足油水混合分离的要求；水滴粗粒化模块5采用316L不锈钢折流板进行水滴粗粒化，CPI模块采用改性PP波纹板，板间距控制为10mm，凹处开孔率为3％，满足水滴聚结后的快速沉降；深度脱水模块7采用尼龙、特氟龙、316L不锈钢纤维混合编制模块，其中三者质量比例为2∶7∶1；深度除油模块7采用的是玻璃纤维、特氟龙纤维、316L不锈钢纤维混合编制模块，其中三者质量比例为6∶3∶1。
(3)排水控制：因注水为0.5％，水量较大，超过了排水口17的处理能力，因此通过界位计控制排水口16、排水口17同时排水；油相通过液面控制器控制液面高度为60％进行外排。
实施效果，采用该发明方法进行改造后，冷低压分离器内油中氢气含量降低了22％，出口水中油含量为80～180ppm，出口油中水含量为210～290ppm，氯离子含量降低至11μg/g，与原有重力沉降分离工艺技术相比，存在以下有益效果：
(1)油中氢气含量降低，氢气回收率提高，降低了下游分馏塔塔顶气相负荷，且提高了经济效益；
(2)出口水中油含量，油中水含量满足了设计要求，消除了油中带水水中带油对下游装置产生的问题；
(3)油出口中氯离子含量降低，降低了下游汽提、分馏塔的腐蚀速率，提高了装置的连续运转周期；
(4)设备占地减小，起到了一定的经济效益。
综上所述仅为发明的较佳实施例而已，并非用来限定本发明的实施范围。即凡依本发明申请专利范围的内容所作的等效变化与修饰，都应为本发明的技术范畴。

Claims (9)

  1. 一种强化冷低压分离器中油水分离和耦合除盐的方法，其特征在于，包括以下步骤：
    步骤1：含水低分油在入口段与脱盐水混合，在此过程混合物中的盐及硫化氢转移到水中，完成初步洗盐后进入T型液气分离器，快速分离低分油中因降压闪蒸出的低分气；其中，所述含水低分油在入口段的压力为0.6～4.5MPa，温度为20～90℃，所述脱盐水的注入量的体积百分比为0～1％；
    步骤2：油水混合物通过二次注水洗涤及整流分布后进入初步分离段，采用亲水性水滴粗粒化模块将油中分散的水滴快速聚结长大，再通过CPI快速分离模块实现油水快速分离，水从底部通过油水界位控制器自动排出或通过隔板左右的连通口进入深度分离腔，油及微量水通过隔板进下个步骤处理；其中，二次注水量的体积百分含量为0～0.5％，整流分布后油水混合物的流动速度为0.005～0.05m/s，CPI模块的波纹板间距为5～18mm，此过程分离出粒径大于30μm的水滴；
    步骤3：油及微量水进入深度分离段后，首先通过重力沉降的方法将粒径较大的水滴分离到底部进入水包，然后通过包括亲水性纤维和亲油性纤维的组合纤维脱水模块进行深度脱水，此过程实现油中夹带的粒径为3～30μm的水滴分离；深度脱水后的油通过液面控制器自动控制排出，分离出的水进入包括亲水性纤维和亲油性纤维的组合纤维除油模块进行除油处理后通过油水界面控制器自动控制外排，此过程经组合纤维模块分离后达到水中含油量小于100mg/L；
    其中，所述组合纤维脱水模块中亲水性纤维占亲油性纤维的比例为5～15％；所述组合纤维除油模块中亲油性纤维占亲水性纤维的比例为10～20％。
  2. 根据权利要求1所述的方法，其特征在于，步骤1所述脱盐水的注入方式为逆流或顺流，注入的水滴粒径为10～50μm。
  3. 根据权利要求1所述的方法，其特征在于，步骤1所述的T型液气分离器入口段的混合液流速为3～6m/s。
  4. 根据权利要求1所述的方法，其特征在于，步骤2所述二次注水的方式为通过内伸管加喷头逆流注水，注水的水滴粒径为30～100μm。
  5. 根据权利要求1所述的方法，其特征在于，步骤2所述的亲水性水滴粗粒化模块和所述CPI快速分离模块采用改性的特氟龙、聚丙烯或者不锈钢材料。
  6. 一种实现权利要求1-5任一所述方法的强化冷低压分离器中油水分离和耦合除盐功能的装置，其特征在于，所述装置包括壳体、设置在所述壳体上的油水气进口，分别与所述油水气进口相连的注水设备和T型液气分离器或旋流脱气器，依次设置于所述壳体内部的二次注水器、整流分布器、油水粗粒化模块、CPI快速分离模块、油水界面控制器、隔板、液面控制器以及处于所述壳体尾部的油相出口；置于所述壳体底部的气体脱液器，所述壳体的顶部具有气相出口；所述壳体的底部还设有水相出口。
  7. 根据权利要求6所述的装置，其特征在于，所述油相出口、气相出口、水相出口上分别设有调节阀。
  8. 根据权利要求6所述的装置，其特征在于，所述气体脱液器内部具有油水界面控制器。
  9. 根据权利要求6所述的装置，其特征在于，所述壳体为卧式或立式。
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