WO2016127274A1 - 一种耦合油气洗涤的混合油水分步分离方法 - Google Patents

一种耦合油气洗涤的混合油水分步分离方法 Download PDF

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WO2016127274A1
WO2016127274A1 PCT/CN2015/000303 CN2015000303W WO2016127274A1 WO 2016127274 A1 WO2016127274 A1 WO 2016127274A1 CN 2015000303 W CN2015000303 W CN 2015000303W WO 2016127274 A1 WO2016127274 A1 WO 2016127274A1
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oil
water
module
separation
separator
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PCT/CN2015/000303
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English (en)
French (fr)
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杨强
卢浩
许萧
刘森
王朝阳
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华东理工大学
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Priority to EP15881436.8A priority Critical patent/EP3257917B1/en
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    • 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
    • B01D17/0211—Separation of non-miscible liquids by sedimentation with baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D39/00—Filtering material for liquid or gaseous fluids
    • B01D39/02—Loose filtering material, e.g. loose fibres
    • 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
    • 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
    • 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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
    • 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
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
    • C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils

Definitions

  • the invention relates to the field of petroleum refining or coal chemical industry, and relates to a method for separating the moisture step of a mixed oil which is coupled with oil and gas washing in a Fischer-Tropsch process.
  • Fischer-Tropsch synthesis is one of the indirect liquefaction technologies of coal. It can be referred to as FT reaction. It is synthesized from syngas (CO and H 2 ) under the conditions of catalyst (mainly iron) and appropriate reaction conditions. Paraffin-based liquid fuel process.
  • the products of Fischer-Tropsch synthetic coal are mainly gasoline, diesel, kerosene and aviation fuel, lubricating oil and paraffin.
  • the Fischer-Tropsch synthetic coal indirect liquefaction product is an oil-water mixture, and the efficient separation of oil and water has an important impact on reducing product cost.
  • the equipment covers a large area, the material is expensive and the efficiency is low.
  • a small amount of hydrocarbons are also contained in the gas phase component discharged after the low pressure separation in the process flow.
  • the washing device is separately washed and recovered, and the operation control system is required, which is high in cost and complicated. Therefore, it is necessary to optimize the current technology by using an efficient and efficient oil-water separation method.
  • the present invention provides a method for moisture separation of a mixed oil coupled with oil and gas washing in a Fischer Tropsch process. Combined with Fischer-Tropsch synthesis oil-water characteristics, it is divided into preliminary separation and depth separation according to the particle size distribution of oil in water and water by step separation method. It is more optimized in preliminary oil dehydration and water deoiling. It is realized by one equipment, the land occupation and supporting system are reduced, and the washing and recovery setting of hydrocarbon-containing gas is set at the inlet coupling to meet the efficient and rapid separation of oil and water, and the effective reduction of land occupation and investment can make up for the existing gravity settlement. The lack of separation methods.
  • a mixed oil moisture step separation method for coupling oil and gas washing comprising the following steps:
  • Step 1 Mixing light oil containing 0.5 to 6% synthetic water (flow rate at the inlet of 1 to 3 m/s) with a low gas containing 0.01 to 2.8% of a trace amount of hydrocarbon, and then entering a trace amount of hydrocarbon light oil
  • the left head of the oil-water preliminary separator is sent to the right head of the oil-water preliminary separator; 0.05-0.5% of the oil is sent to the right head of the oil-water preliminary separator;
  • the operating pressure of the oil-water preliminary separator is 0.3-4.5 MPa, and the temperature is 20 to 60 ° C;
  • Step 2 After the components of step 1 enter the oil-water preliminary separator, firstly, rapid liquid-gas separation is realized in the T-type liquid-gas separator, and the separated low-gas separation is discharged from the top of the oil-water preliminary separator;
  • the water-containing light oil flows from the left head of the oil-water preliminary separator to the right at a flow rate of 0.005 to 0.02 m/s, and is rapidly dehydrated by the first CPI oil-water rapid separation module and the hydrophilic coarse granulation module in turn, and separated.
  • the oily sewage flows from the right head of the oil-water preliminary separator to the left, and is sequentially subjected to rapid degreasing by a second CPI oil-water rapid separation module and a lipophilic coarse granulation module to separate oil droplets having a particle diameter larger than 25 ⁇ m.
  • the post-sewage contains 0.03 ⁇ 0.6% oil and continues to flow to the left to the right side of the partition.
  • the light oil separated from the upper part of the partition and the left side of the partition is mixed and discharged, and enters the deep degreaser.
  • the oil droplets having a particle diameter of 1 to 25 ⁇ m are removed, and the oil content of the sewage at this time is less than 0.01%.
  • the deep dehydrator in the step 2 has a combined fiber dehydration module comprising a hydrophilic fiber and a lipophilic fiber, wherein the ratio of the hydrophilic fiber to the lipophilic fiber in the combined fiber dehydration module is 5 to 15%;
  • the oiler has a combined fiber degreasing module comprising a hydrophilic fiber and a lipophilic fiber, wherein the lipophilic fiber in the combined fiber degreasing module accounts for 10 to 20% of the hydrophilic fiber.
  • the mixing method of the light oil and the low gas separation in step 1 is a countercurrent or a downstream flow, and a conventional gas-liquid mixer is disposed after the injection section.
  • the flow rate of the mixed liquid in the inlet section of the T-type liquid gas separator described in the step 2 is 3 to 6 m/s.
  • the first CPI oil-water rapid separation module and the hydrophilic coarse granulation module described in step 2 have a water bag; the second CPI oil-water rapid separation module and the lipophilic coarse granulation module are connected and disposed.
  • the hydrophilic coarse granulation module and the first and second CPI rapid separation modules of step 2 are made of modified Teflon, polypropylene or stainless steel.
  • the bottom of the deep dewatering device described in step 2 has a water bag outlet, and a combined fiber degreasing module is further disposed at the water bag outlet; the top of the deep degreaser has oil bagout at the oil bag outlet Also has a group Fiber dewatering module.
  • the composite fiber module built in the deep dewatering device or the deep degreaser adopts a patented weaving method disclosed in CN103952852A (an omega fiber weaving method suitable for deep separation of oil and water).
  • CPI high-efficiency corrugated plate coalescence separation
  • oil-water rapid separation module uses open-hole corrugated plate material with oleophilic hydrophobic (or hydrophilic oleophobic, suitable for dehydration process), and will be “shallow pool principle” and “poly The knotting technique is effectively combined, as shown in Figure 1: when the oily wastewater passes through the coalescing plate pile, the tortuous path of the corrugated plate forces the water flow to form a flow state of approximately sinusoidal wave, thereby increasing the collision probability between the oil beads and promoting the small oil. The condensation of the drops. Since the corrugated plate is wavy, the flow direction is constantly changing, increasing the probability of collision and making the small oil bead larger.
  • the oil bead settling velocity is proportional to the square of the oil bead particle size, and the large oil bead specific surface area becomes smaller and The surface tension of water is relatively small, thus accelerating the oil bead settling and achieving the purpose of oil-water separation.
  • the oil and gas washing is integrated into the preliminary separator.
  • the preliminary separator reuses the T-type liquid-gas separation technology.
  • the gas is rapidly degassed by the centrifugal force of the T-tube liquid rotating, the structure is simple and the separation efficiency is higher than the gravity settlement.
  • the liquid moves from the inside to the outside in the radial section, and moves from the top to the bottom in the vertical section to complete the secondary washing action, and the washing action of the two processes of combining and mixing and separating;
  • the present invention converts CPI, coarse granulation, and the characteristics of Fischer-Tropsch oil and water.
  • the combined fiber separation technology is combined and integrated, the separation time is short, and the separation efficiency is improved (the emulsified oil cannot be separated in gravity sedimentation), the resource utilization rate is improved, and the oil content in the wastewater is reduced, and the processing difficulty in the next process is reduced.
  • the method adopted by the invention has the characteristics of simple, high efficiency and wide adaptability, and satisfies the requirements of oil-water separation of the current Fischer-Tropsch synthesis, and integrates the function of washing hydrocarbon components in the recovered gas, and can also be applied to coal chemical industry. Oil-water separation of similar processes.
  • Figure 1 is a schematic diagram of the principle of CPI rapid degreasing or dewatering (lower opening);
  • Embodiment 2 is a process flow diagram of Embodiment 1;
  • Fig. 3 is a schematic structural view of the apparatus used in the first embodiment.
  • hydrocarbon-containing gas inlet 20 hydrocarbon-containing gas inlet; 30 gas-liquid mixer; 40 T-type liquid-gas separator;
  • the fuel oil flow rate of a coal chemical plant Fischer-Tropsch synthesis unit is 50t/h after high pressure separator, and the oily wastewater flow rate is 7t/h.
  • the light oil contains about 3-4% water, and the oily wastewater contains about 2 ⁇ 3% oil, which is rich.
  • the hydrocarbon gas is about 4t/h.
  • the following methods are used for oil-water separation: about 3-4% of the light oil separated by the high-pressure separator enters the preliminary oil-water separator for sedimentation and dehydration.
  • the designed settling time is 0.5 hours. Reach The water is about 0.5-1.5% and sent to the dehydration tank for dehydration for a long time.
  • the dehydration time is not less than 8 hours, the water drop is about 0.1% or less, and then sent to the oil storage tank; and the oil-containing synthesis separated at the bottom of the high-pressure separator
  • the water enters the sewage buffer tank, and the water settled from the preliminary oil-water separator is mixed and buffered in the sewage buffer tank, and then pumped to the grease trap for long-term settlement and degreasing.
  • the oil separation time is more than 24 hours, and the oil is separated.
  • the sewage is about 0.05 or so, it is sent to the sewage treatment plant, and the sewage recovered from the top of the grease trap is sent to the underground sewage tank for recycling, and is reused after treatment. Due to the large area of the dewatering tank and the grease trap, the two equipments are placed outside the core production unit, and the pump is used to transport the oil and water through the pipeline.
  • the oil separated in the high-pressure separator contains water and oil in the water, and there is oil-water emulsification. Therefore, the existing separation method uses conventional gravity sedimentation to improve the separation of oil and water through long-term sedimentation. The effect is that the equipment is large and the separation efficiency is low, and the equipment has a large floor area, and the related supporting foundation and piping are also expensive, and therefore need to be modified.
  • the process flow of this embodiment is as shown in FIG. 2, and the oil-water separation is carried out by a two-stage separation method, and the oil 2 containing 0.5 to 6% of synthetic water (flow rate at the inlet is 1 to 3 m/s) and 0.01 to 0.01 2.8% of the trace hydrocarbon hydrocarbon-containing gas 1 is mixed and washed, wherein the light oil entering the trace hydrocarbon is sent to the left head of the oil-water preliminary separator, and the oil containing 0.05-0.5% of the oil is sent to the right side of the oil-water preliminary separator.
  • the head; the oil-water preliminary separator has an operating pressure of 0.3 to 4.5 MPa and a temperature of 20 to 60 °C.
  • the rapid liquid-gas separation is first performed in the T-type liquid-gas separator 40 (Fig. 3), and the separated dehydrogenated gas 3 is discharged from the top of the oil-water preliminary separator.
  • the water-containing light oil flows from the left head of the oil-water preliminary separator to the right at a flow rate of 0.005 to 0.02 m/s, and is rapidly dehydrated by the rapid dehydration CPI module 50 and the hydrophilic coarse granulation module 60 in sequence, and the particle size is separated by more than 30 ⁇ m water droplets, the separated light oil contains 0.05-0.5% water and continues to flow to the left to the left side of the separator 70, enters the deep dehydrator, and removes water droplets with a particle size of 3-30 ⁇ m in the deep degasser.
  • the light oil obtained at this time has a water content of less than 0.02%, that is, 8 and 9 in Fig. 2;
  • the sewage 4 containing 0.05-0.5% of oil flows from the right head of the oil-water preliminary separator to the left, and is rapidly degreased by the quick degreasing CPI module 102 and the lipophilic coarse granulation module 90, and the particle size is larger than 25 ⁇ m.
  • the oil droplets, the sewage 7 containing 0.03 to 0.6% oil after separation continues to flow to the left to the right side of the partition 70, and the light oil separated from the upper part of the partition 70 and the left side of the partition 70 is mixed and discharged, and the deep degreasing is entered.
  • the oil content of the sewage is less than 0.01%, that is, 10 in Figure 2.
  • the specific implementation process is: the light oil containing about 3-4% water separated by the high pressure separator is first passed through the gas-liquid mixer 30 through the hydrous oil inlet 101 and the hydrocarbon-rich gas inlet 20. After washing, washing and then entering the T-type liquid-gas separator 40 at the inlet of the left side of the preliminary oil-water separator to perform liquid-gas separation, and completing the two-stage dehydrocarbonation treatment, and the purified hydrocarbon-rich gas is discharged from the gas phase outlet 8;
  • the light oil is quickly removed from the free-dried CPI module 50 of 400 mm length and the free water having a particle size larger than 80 ⁇ m, and then the water droplets entrained in the oil are aggregated and intercepted by the hydrophilic coarse granulation module 60 of the 200 mm section.
  • the process completes the coarse granulation growth of free water above 30 ⁇ m and intercepts and separates, and the liquid phase flow rate of the process is controlled to be no more than 0.02 m/s, and after the separation reaches 0.15% of the water in the oil, the separator 70 is not exceeded.
  • the right side is discharged, and the separated water settles into the water bag 120 due to the difference in density; about 2% to 3% of the oil containing oil enters from the right side of the preliminary separator, passes through the rapid degreasing CPI module 102, and is lipophilic.
  • Granulation module 90 After rapid degreasing, it flows to the right side of the partition plate 70, and the liquid phase flow speed during this process is controlled to be no more than 0.025 m/s, and the separated dirty oil is mixed and discharged from the light oil separated from the upper portion of the partition plate 70, and separated.
  • the oil content of the sewage is not more than 0.1%, and the sewage is discharged from the right side of the partition 70 to the deep degreaser; the light oil separated by the preliminary separator enters the deep dehydrator, and the combined fiber dehydration module is set in the deep dehydrator. 14-2 (containing hydrophilic fiber and lipophilic fiber) for deep dehydration.
  • This process realizes the separation of water droplets with a particle size of 3-30 ⁇ m entrained in the oil.
  • the water content of light oil is less than 0.02%, and the removed small amount of water is combined.
  • the fiber degreasing module 13-2 containing hydrophilic fiber and lipophilic fiber
  • it reaches not less than 0.01% in water and is sent to the sewage treatment plant; the sewage separated by the preliminary separator enters the deep degreaser and is removed by depth.
  • the combined fiber degreasing module 13-1 (containing hydrophilic fiber and lipophilic fiber) provided in the oiler performs deep degreasing, and the process realizes separation of oil droplets having an particle diameter of 1 to 25 ⁇ m entrained in the oil, and the oil content of the sewage is less than 0.005% post After treatment in the sewage treatment plant, a small amount of separated oil is further dehydrated by the fiber dehydration module 14-1 (containing hydrophilic fibers and lipophilic fibers) to reach the underground oil tank after the water content of the sewage is less than 0.05%.
  • the ratio of hydrophilic fibers to lipophilic fibers in the combined fiber dewatering module is 12%, and the ratio of lipophilic fibers to hydrophilic fibers in the combined fiber degreasing module is 16%, and the liquid phase velocity in the deep degreaser Not more than 0.022 m/s, the liquid phase flow rate in the deep dehydrator is not more than 0.015 m/s.
  • the effect of the implementation is that after the modification by the method of the invention, the equipment occupies less area and the separation efficiency is improved.
  • the total separation time of the previous oil dehydration was reduced to less than 10 minutes in 8.5 hours, and the total separation time of degreasing was 24 hours.
  • Reduced to less than 8 minutes the equipment reduces investment and can be placed in the production equipment area, reducing the cost of the external pump, pipeline and related facilities; secondly, the separation efficiency is improved, after deep degreasing, dehydration and oil
  • the water content is reduced to less than 200ppm, and the oil content in the water is reduced to less than 50ppm.
  • the oil recovery efficiency is improved, and the investment in the subsequent sewage treatment facilities is reduced. Good energy-saving and resource-reducing resources recovery; finally, some of the hydrocarbons are recovered through the gas scrubbing facility set up by the preliminary separator, which also has economic benefits.

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Abstract

本发明涉及一种耦合油气洗涤的混合油水分步分离方法。首先，含0.5~6%合成水的轻油与含微量烃的低分气混合洗涤烃类组分，之后从左侧封头进入油水初步分离器，含油0.05~0.5%的污水从右侧封头进入；净化低分气从顶部排出，混合液体排出进入深度脱水器，排出轻油中含水约0.05~0.5%；左侧污水进入水包排出，右侧除油后的污水在靠近隔板的右侧排出进入深度除油器，排出水中含油约0.03~0.6%；依靠深度脱水、除油器中以特殊方式编织的组合纤维模块进行深度除油、脱水后，轻油中含水小于0.02%，污水中含油小于0.01%后分别外送。本发明采用组合油水分离及分步分离的方法能快速高效实现油品脱水及污水除油，且最大程度回收油品。

Description

一种耦合油气洗涤的混合油水分步分离方法 技术领域
本发明涉及石油炼制或者煤化工领域，涉及费托工艺中一种耦合油气洗涤的混合油水分步分离的方法。
背景技术
费托合成(Fischer-Tropsch synthesis)是煤间接液化技术之一，可简称为FT反应，它以合成气(CO和H2)为原料在催化剂(主要是铁系)和适当反应条件下合成以石蜡烃为主的液体燃料的工艺过程。费托合成煤制油的产品主要有汽油、柴油、煤油及航空燃料、润滑油和石蜡等。费托合成煤间接液化产品为油水混合物，油水的高效分离对降低产品成本有着重要影响。
目前在费托合成中重要采用重力沉降的方法进行分离(费托合成工艺油水分离器的工艺设计，化工设计，2010，20(1))自反应器出来后经高压分离器的沉降作用分出含水油及含油水，进入卧式油水分离器进行进一步沉降分离，分离后再进入大罐沉降分离，由于费托合成的操作条件，油水乳化现象比较严重，因重力沉降分离只能有效分离粒径大于50μm游离态的油滴或者水滴，因此一般经初步油水分离后采用大罐静置沉降分离设计时间超过8小时。设备占地面积大、材料耗费大且效率低。此外经工艺流程中低压分离后排出的气相组分中也含有少量烃类，一般单独设洗涤装置洗涤回收，需配套操作控制系统，造价高且比较复杂。因此需要采用型高效的油水分离方法对目前技术进行优化。
发明内容
鉴于上述问题，本发明提供费托工艺中一种耦合油气洗涤的混合油水分步分离的方法。其结合费托合成油水特性，采用分步分离的方法按照油中水和水中油的粒径分布分为初步分离和深度的逐级分离，更为优化的是在初步的油脱水和水脱油采用一个设备实现，占地及配套系统均减少，且在入口耦合设置了含烃气体的洗涤回收设置，满足油水高效快速分离的同时，有效减小的占地及投资，弥补了现有重力沉降分离方法的不足。
具体的技术方案为：
一种耦合油气洗涤的混合油水分步分离方法，包括以下步骤：
步骤1：将含0.5～6％合成水的轻油(在入口处的流速为1～3m/s)与含0.01～2.8％微量烃的低分气混合洗涤后，其中进入微量烃的轻油送入油水初步分离器的左侧封头，含油0.05～0.5％的污水则送入所述油水初步分离器的右侧封头；所述油水初步分离器的操作压力为0.3～4.5MPa，温度为20～60℃；
步骤2：步骤1的各组分进入所述油水初步分离器后首先在T型液气分离器中实现快速液气分离，分离出的低分气从所述油水初步分离器的顶部排出；
含水轻油以流速0.005～0.02m/s从所述油水初步分离器的左侧封头向右流动，依次通过第一CPI油水快速分离模块、亲水性粗粒化模块进行快速脱水，分离出粒径大于30μm的水滴，分离后的轻油中含水0.05～0.5％并继续向右流动到隔板左侧排出，进入深度脱水器，在所述深度脱气器中脱除粒径为3～30μm的水滴，此时得到的轻油含水量小于0.02％；
含油污水从所述油水初步分离器的右侧封头向左流动，依次通过第二CPI油水快速分离模块、亲油性粗粒化模块进行快速除油，分离出粒径大于25μm的油滴，分离后污水中含油0.03～0.6％并继续向左流动到隔板的右侧，从隔板上部与隔板左侧分离后的轻油混合排出，进入深度除油器，在所述深度除油器中脱除粒径为1～25μm的油滴，此时的污水含油量小于0.01％。
步骤2中所述深度脱水器具有包括亲水性纤维和亲油性纤维的组合纤维脱水模块，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％；所述深度除油器具有包括亲水性纤维和亲油性纤维的组合纤维除油模块，所述组合纤维除油模块中亲油性纤维占亲水性纤维比例为10～20％。
步骤1所述轻油与低分气的混合方式是逆流或顺流，注入段后设置常规气液混合器。
步骤2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所述的第一CPI油水快速分离模块和所述亲水性粗粒化模块之间具有水包；所述第二CPI油水快速分离模块和所述亲油性粗粒化模块连接设置。
步骤2所述的亲水性粗粒化模块和所述第一、第二CPI快速分离模块采用改性特氟龙、聚丙烯或者不锈钢材料。
步骤2所述的深度脱水器的底部具有水包出口，在所述水包出口还设有组合纤维除油模块；所述的深度除油器的顶部具有油包出，在所述油包出口还设有组 合纤维脱水模块。
所述的深度脱水器或者深度除油器中内置的组合纤维模块采用公开号为CN103952852A(一种适用于油水深度分离的Ω型纤维编织方法)专利编织方法。
其中，CPI(高效波纹板聚结分离)油水快速分离模块选用表面具有亲油疏水(或亲水疏油，适用于脱水过程)性质的开孔波纹板材料，将“浅池原理”和“聚结技术”有效相结合，如图1所示：当含油废水通过聚结板堆时波纹板的曲折通道迫使水流形成近似正弦波的流态，从而增大油珠间的碰撞几率，促使小油滴的聚结。由于波纹板是波浪形的，流向不断发生变化，增加碰撞几率使小油珠变大，根据Stocks公式，油珠沉降速度与油珠粒径的平方成正比，且大油珠比表面积变小与水的表面张力相对变小，因此加速了油珠沉降，达到了油水分离的目的。
本发明的有益效果在于：
(1)在设计上采用了分布分级分离的思路，根据费托合成的油水性质：即大部分游离态、分散态油水混合物采用PPI、粗粒化方法先先快速分离，少量为乳化态油水混合物(占总量的0.1～3％)通过组合纤维编织模块深度分离的方法进行处理。相比较目前重力沉降的方法具有分离速度快、效率高的优势，此外该方法采用分步逐级分离可以最大限度的发挥每个技术的高效性和适应性，如初步分离后，油中水含量降低，这样通过组合纤维聚结分离，组合纤维模块能发挥对低浓度含量的快速高效分离，且能保护该模块的长周期运行；
(2)将油气洗涤集成于初步分离器，初步分离器重采用T型液气分离技术，一方面气体通过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型分离器的洗涤混合，控制T型管入口流速为3～6m/s时，气液两相在T型管中受到旋转离心力的作用，由于油水密度差的原因，液体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，能完成二次洗涤作用，结合和混合与分离两个过程的洗涤作用；
(3)将油初步脱水与水初步脱油两个功能集成于一个初步分离器中，可以减少一个设备，所需配套的配管、控制、阀门及占地都减少，起到降低投资的作用。
(4)更为重要的是，本发明根据费托合成油水的特性将CPI、粗粒化以及 组合纤维分离技术进行了组合集成，分离时间短，且分离效率提高(乳化油在重力沉降中不能分离)，提高了资源利用率，以及降低了废水中的油含量，下个过程处理难度降低。
本发明采用的方法具有简单、高效及适应性宽的特点，在功能上满足了目前费托合成的油水分离要求，且集成了洗涤回收气体中烃类组份的功能，也可应用于煤化工同类过程的油水分离。
附图说明
图1是CPI快速除油或脱水(下部开孔)原理示意；
图2是实施例1的工艺流程图；
图3是实施例1所使用装置的结构示意图。
符号说明
1 含烃气体；2 含0.5～6％合成水的油；3 脱烃后气体；
4 含油0.05～0.5％的污水；5 含0.03～0.6％油的污水；
6 含0.05～0.5％水的油；7 含0.03～0.6％油的污水；
8 含水小于0.02％的油；9 含水小于0.02％的油(去污油罐)；
10 含油小于0.01％的污水；101 含水油进口；
20 含烃类气体入口；30 气液混合器；40 T型液气分离器；
50 快速脱水CPI模块；60 亲水性粗粒化模块；70 隔板；
80 气相出口；90 亲油性粗粒化模块；102 快速除油CPI模块；
110 含油废水进口；120 水包；13-1、13-2 组合纤维除油模块；
14-1、14-2 组合纤维脱水模块。
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。
对比例1
某煤化工厂费托合成装置经高压分离器后轻油流量为50t/h，含油废水流量7t/h，其中轻油中含水约3～4％，含油废水中含油约2～3％，产生富烃气约4t/h，目前采用以下方法进行油水分离：高压分离器分离出来的含水约3～4％的轻油进入初步油水分离器进行沉降脱水，此过程设计沉降时间为0.5小时，沉降后达到 含水约0.5～1.5％送入脱水罐进行长时间脱水，此过程脱水时间不小于8个小时，含水降为约0.1％以下后送到油品储罐；而高压分离器底部分离出的含油合成水进入污水缓冲罐，与初步油水分离器沉降出的水在污水缓冲罐进行混合缓冲，之后由泵送到隔油罐进行长时间沉降除油，此过程隔油时间为24小时以上，隔油后污水含油约0.05左右后送到污水处理厂，而隔油罐顶部回收的污油送往地下污油罐进行回收，处理后回用。由于脱水罐、隔油罐占地面积大，因此该两个设备放到核心生产装置之外进行，中间采用泵通过管道将油、水输送过去。
由于费托合成的工艺原因，在高压分离器分离出的油中含水、水中含油，且存在油水乳化现象，因此现有分离方法采用常规重力沉降方式只能通过长时间的沉降来提高油水的分离效果，存在设备大、分离效率低的问题，且设备大占地面积大，相关配套的基础、配管等费用也高，因此需进行改造。
实施例1
本实施例的工艺流程如图2所示，采用两级分离的方法进行油水分离，将含0.5～6％合成水的油2(在入口处的流速为1～3m/s)与含0.01～2.8％微量烃的含烃气体1混合洗涤后，其中进入微量烃的轻油送入油水初步分离器的左侧封头，含油0.05～0.5％的污水4则送入油水初步分离器的右侧封头；油水初步分离器的操作压力为0.3～4.5MPa，温度为20～60℃。
然后，各组分进入油水初步分离器后首先在T型液气分离器40(如图3)中实现快速液气分离，分离出的脱烃后气体3从油水初步分离器的顶部排出。
含水轻油以流速0.005～0.02m/s从油水初步分离器的左侧封头向右流动，依次通过快速脱水CPI模块50、亲水性粗粒化模块60进行快速脱水，分离出粒径大于30μm的水滴，分离后的轻油中含水0.05～0.5％并继续向右流动到隔板70左侧排出，进入深度脱水器，在深度脱气器中脱除粒径为3～30μm的水滴，此时得到的轻油含水量小于0.02％，即图2中的8和9；
含油0.05～0.5％的污水4从油水初步分离器的右侧封头向左流动，依次通过快速除油CPI模块102、亲油性粗粒化模块90进行快速除油，分离出粒径大于25μm的油滴，分离后中含0.03～0.6％油的污水7继续向左流动到隔板70的右侧，从隔板70上部与隔板70左侧分离后的轻油混合排出，进入深度除油器，在深度除油器中脱除粒径为1～25μm的油滴，此时的污水含油量小于0.01％，即 图2中的10。
结合图3，具体实施过程为：高压分离器分离出来的含水约3～4％的轻油首先通过含水油进口101与含烃类气体入口20进来的富烃气通过气液混合器30进行顺流洗涤，洗涤后再进入初步油水分离器左侧入口处的T型液气分离器40进行液气分离，并完成2次洗涤脱烃处理，净化后的富烃气从气相出口8排出；含水轻油通过400mm段长的快速脱水CPI模块50进行快速脱除粒径大于80μm游离水，之后再通过200mm段的亲水性粗粒化模块60将油中夹带的水滴进行聚结长大并拦截，此过程完成30μm以上游离水的粗粒化长大并拦截分离，控制此过程的液相流动速度不大于0.02m/s，分离后达到油中带水不超过的0.15％后从隔板70的右侧排出，分离出的水由于密度差的作用沉降进入水包120；含油约2％～3％的废水从初步分离器的右侧进入，依次通过快速除油CPI模块102、亲油性粗粒化模块90进行快速除油后流动到隔板70的右侧，控制此过程液相流动速度不大于0.025m/s，分离出的污油从隔板70上部与左侧分离后的轻油混合排出，分离后的污水中油含量不大于0.1％，污水从靠近隔板70的右侧排出到深度除油器；经初步分离器分离后的轻油进入深度脱水器，通过深度脱水器中设置的组合纤维脱水模块14-2(含亲水性纤维和亲油性纤维)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，轻油含水量小于0.02％，脱除的少量水再经组合纤维除油模块13-2(含亲水性纤维和亲油性纤维)处理后达到水中含油不大于0.01％后送到污水处理厂；经初步分离器分离后的污水进入深度除油器，通过深度除油器中设置的组合纤维除油模块13-1(含亲水性纤维和亲油性纤维)进行深度除油，此过程实现油中夹带的粒径为1～25μm的油滴分离，污水含油量小于0.005％后送到污水处理厂进行处理，分离出的少量污油再经纤维脱水模块14-1(含亲水性纤维和亲油性纤维)进行深度脱水达到污油含水量小于0.05％后送到地下污油罐进行回收；其中组合纤维脱水模块中亲水性纤维占亲油性纤维的比例为12％，组合纤维除油模块中亲油性纤维占亲水性纤维的比例为16％，深度除油器内液相流速不大于0.022m/s，深度脱水器内液相流速不大于0.015m/s。
实施效果，采用该发明方法进行改造后，设备占地减小，分离效率提高。先前油脱水总分离时间8.5小时减小到10分钟以内，而除油总分离时间由24小时 减小到8分钟以内，设备减小投资降低且均能布置在生产装置区，减小了外输配套泵、管线及相关设施的造价；其次分离效率提高，经深度除油、脱水后油中水含量降低到200ppm以内，水中油含量降低到50ppm以内，对比以前大罐沉降的油中水含量1000ppm，水中油含量500ppm来说，油品回收效率提高，后续污水处理设施的投资降低，起到了良好的节能降耗资源回收的作用；最后通过初步分离器设置的气体洗涤设施，回收了部分烃，也起到了经济效益。
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 (7)

  1. 一种耦合油气洗涤的混合油水分步分离方法，其特征在于，包括以下步骤：
    步骤1：将含0.5～6％合成水的轻油与含0.01～2.8％微量烃的低分气混合洗涤后，其中进入微量烃的轻油送入油水初步分离器的左侧封头，含油0.05～0.5％的污水则送入所述油水初步分离器的右侧封头；所述油水初步分离器的操作压力为0.3～4.5MPa，温度为20～60℃；
    步骤2：步骤1的各组分进入所述油水初步分离器后首先在T型液气分离器中实现快速液气分离，分离出的低分气从所述油水初步分离器的顶部排出；
    含水轻油以流速0.005～0.02m/s从所述油水初步分离器的左侧封头向右流动，依次通过第一CPI油水快速分离模块、亲水性粗粒化模块进行快速脱水，分离出粒径大于30μm的水滴，分离后的轻油中含水0.05～0.5％并继续向右流动到隔板左侧排出，进入深度脱水器，在所述深度脱气器中脱除粒径为3～30μm的水滴，此时得到的轻油含水量小于0.02％；
    含油污水从所述油水初步分离器的右侧封头向左流动，依次通过第二CPI油水快速分离模块、亲油性粗粒化模块进行快速除油，分离出粒径大于25μm的油滴，分离后污水中含油0.03～0.6％并继续向左流动到隔板的右侧，从隔板上部与隔板左侧分离后的轻油混合排出，进入深度除油器，在所述深度除油器中脱除粒径为1～25μm的油滴，此时的污水含油量小于0.01％。
  2. 根据权利要求1所述的混合油水分步分离方法，其特征在于，步骤2中所述深度脱水器具有包括亲水性纤维和亲油性纤维的组合纤维脱水模块，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％；所述深度除油器具有包括亲水性纤维和亲油性纤维的组合纤维除油模块，所述组合纤维除油模块中亲油性纤维占亲水性纤维比例为10～20％。
  3. 根据权利要求1所述的混合油水分步分离方法，其特征在于，步骤1所述轻油与低分气的混合方式是逆流或顺流，注入段后设置常规气液混合器。
  4. 根据权利要求1所述的混合油水分步分离方法，其特征在于，步骤2所述的T型液气分离器入口段的混合液流速为3～6m/s。
  5. 根据权利要求1所述的混合油水分步分离方法，其特征在于，步骤2所述的第一CPI油水快速分离模块和所述亲水性粗粒化模块之间具有水包；所述第二 CPI油水快速分离模块和所述亲油性粗粒化模块连接设置。
  6. 根据权利要求1所述的混合油水分步分离方法，其特征在于，步骤2所述的亲水性粗粒化模块和所述第一、第二CPI快速分离模块采用改性特氟龙、聚丙烯或者不锈钢材料。
  7. 根据权利要求2所述的混合油水分步分离方法，其特征在于，步骤2所述的深度脱水器的底部具有水包出口，在所述水包出口还设有组合纤维除油模块；所述的深度除油器的顶部具有油包出，在所述油包出口还设有组合纤维脱水模块。
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CN111450576A (zh) * 2020-04-15 2020-07-28 中国石油化工股份有限公司 一种油水分离装置及油水分离方法
CN111763166A (zh) * 2020-07-14 2020-10-13 中国石油化工股份有限公司 一种chppo装置脱酸除钠的系统和方法
CN111892523A (zh) * 2020-07-14 2020-11-06 中国石油化工股份有限公司 一种chppo装置分离除酸脱钠的方法
CN112062216A (zh) * 2020-09-17 2020-12-11 华东理工大学 基于纤维异质结的双乳液滴内循环流动的破乳方法和装置
CN112362563A (zh) * 2020-10-29 2021-02-12 中国石油天然气集团有限公司 一种评价油水耦合介质中石油管材耐蚀性能的装置
CN112624410A (zh) * 2020-12-17 2021-04-09 华东理工大学 油田采出水深度净化方法与装置
CN113072130A (zh) * 2021-04-28 2021-07-06 新乡市万和过滤技术股份公司 舱底油水分离器
CN113486579A (zh) * 2021-06-29 2021-10-08 中国石油大学(北京) 基于液滴微观分布衍化的油水分离预测方法及装置
CN114278861A (zh) * 2020-12-31 2022-04-05 官天日 一种多相流分输处理的方法、控制机构以及装置
CN114409169A (zh) * 2022-01-27 2022-04-29 陕西华祥能源科技集团有限公司 一种煤气站酚水除油蒸发处理装置及工艺
CN114477494A (zh) * 2022-01-18 2022-05-13 华东理工大学 一种脱气及轻重油分级处理的酚氨废水处理装置和工艺
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
CN115105864A (zh) * 2022-07-15 2022-09-27 广西上林县林发松香有限公司 一种高效油水分离器及其提取松节油的方法
CN116059699A (zh) * 2021-11-04 2023-05-05 中国石油化工股份有限公司 一种聚结除油器
CN117843080A (zh) * 2024-03-07 2024-04-09 陕西嘉丰自控设备技术有限公司 一种油田水处理装置

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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
CN111450576A (zh) * 2020-04-15 2020-07-28 中国石油化工股份有限公司 一种油水分离装置及油水分离方法
CN111763166A (zh) * 2020-07-14 2020-10-13 中国石油化工股份有限公司 一种chppo装置脱酸除钠的系统和方法
CN111892523A (zh) * 2020-07-14 2020-11-06 中国石油化工股份有限公司 一种chppo装置分离除酸脱钠的方法
CN112062216A (zh) * 2020-09-17 2020-12-11 华东理工大学 基于纤维异质结的双乳液滴内循环流动的破乳方法和装置
CN112362563B (zh) * 2020-10-29 2023-11-28 中国石油天然气集团有限公司 一种评价油水耦合介质中石油管材耐蚀性能的装置
CN112362563A (zh) * 2020-10-29 2021-02-12 中国石油天然气集团有限公司 一种评价油水耦合介质中石油管材耐蚀性能的装置
CN112624410A (zh) * 2020-12-17 2021-04-09 华东理工大学 油田采出水深度净化方法与装置
CN114278861A (zh) * 2020-12-31 2022-04-05 官天日 一种多相流分输处理的方法、控制机构以及装置
CN114278861B (zh) * 2020-12-31 2024-03-01 广东管辅能源科技有限公司 一种多相流分输处理的方法、控制机构以及装置
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
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
CN113072130B (zh) * 2021-04-28 2024-04-26 新乡市万和过滤技术股份公司 舱底油水分离器
CN113072130A (zh) * 2021-04-28 2021-07-06 新乡市万和过滤技术股份公司 舱底油水分离器
CN113486579B (zh) * 2021-06-29 2023-06-09 中国石油大学(北京) 基于液滴微观分布衍化的油水分离预测方法及装置
CN113486579A (zh) * 2021-06-29 2021-10-08 中国石油大学(北京) 基于液滴微观分布衍化的油水分离预测方法及装置
CN116059699A (zh) * 2021-11-04 2023-05-05 中国石油化工股份有限公司 一种聚结除油器
CN114477494B (zh) * 2022-01-18 2023-07-25 华东理工大学 一种脱气及轻重油分级处理的酚氨废水处理装置和工艺
CN114477494A (zh) * 2022-01-18 2022-05-13 华东理工大学 一种脱气及轻重油分级处理的酚氨废水处理装置和工艺
CN114409169A (zh) * 2022-01-27 2022-04-29 陕西华祥能源科技集团有限公司 一种煤气站酚水除油蒸发处理装置及工艺
CN115105864A (zh) * 2022-07-15 2022-09-27 广西上林县林发松香有限公司 一种高效油水分离器及其提取松节油的方法
CN117843080A (zh) * 2024-03-07 2024-04-09 陕西嘉丰自控设备技术有限公司 一种油田水处理装置
CN117843080B (zh) * 2024-03-07 2024-05-28 陕西嘉丰自控设备技术有限公司 一种油田水处理装置

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