WO2020098193A1 - 取消气浮的含油污水预处理方法和装置 - Google Patents

取消气浮的含油污水预处理方法和装置 Download PDF

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Publication number
WO2020098193A1
WO2020098193A1 PCT/CN2019/078618 CN2019078618W WO2020098193A1 WO 2020098193 A1 WO2020098193 A1 WO 2020098193A1 CN 2019078618 W CN2019078618 W CN 2019078618W WO 2020098193 A1 WO2020098193 A1 WO 2020098193A1
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separation
oil
oily sewage
fluidized bed
shape
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PCT/CN2019/078618
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English (en)
French (fr)
Inventor
汪华林
孙玉萧
胡建东
刘毅
俞惠庆
白海洋
虞碧川
王盾
江霞
白志山
杨强
陈建琦
袁威
沈其松
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上海华畅环保设备发展有限公司
四川大学
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Priority to EP19884607.3A priority Critical patent/EP3882220B1/en
Priority to US17/293,730 priority patent/US12017939B2/en
Publication of WO2020098193A1 publication Critical patent/WO2020098193A1/zh

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    • 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
    • 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
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • 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
    • 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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B04C2009/004—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with internal filters, in the cyclone chamber or in the vortex finder
    • 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
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil
    • C02F2101/322—Volatile compounds, e.g. benzene
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil
    • C02F2101/325—Emulsions
    • 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)
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/14—Maintenance of water treatment installations
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters

Definitions

  • the present disclosure belongs to the fields of petrochemical industry and environmental protection, and relates to an oily sewage treatment technology. Specifically, the present disclosure relates to an oily sewage treatment method that combines sedimentation separation, ebullated bed separation, and shape coalescence separation. The present disclosure also relates to an oily sewage treatment device.
  • oil-water pretreatment means have a common problem: to scale wastewater treatment and 1000m 3 / h, which pharmaceutical consumption grease + flotation process follows: the PAC (aluminum oxide polymerization) consumption of 6080t, FeCl 3 annual consumption 2800t , PAM (polyacrylamide) consumes 115t per year, the chemical consumption is huge, the cost is high, and it is easy to cause secondary pollution; the flotation cell needs to be aerated, and its VOCs (volatile organic compounds) emissions can reach 8100Nm 3 / h In the process of operation, the structure of the structure is large, which is easy to cause leakage of VOCs. In addition, the flotation slag output of the flotation tank is about 500t per month, which generates a large amount of oily hazardous waste.
  • US patent application US20120132588A1 discloses a treatment method for oil-containing wastewater, using electrochemical flocculation and flotation as pretreatment methods, and membrane distillation to treat pretreated effluent, which can be used as raw water for steam generation.
  • this method has the problem of large energy consumption.
  • Chinese patent CN104843817B discloses a horizontal air-floating coupled corrugated board degreasing method and device, which adopts an optimized combination method of multi-layer inclined plate unit and horizontal air-floating coupling technology to realize the separation of three phases with high efficiency, rapidity and low energy consumption , Suitable for sewage treatment, crude oil mining and other oily wastewater treatment processes.
  • Chinese patent application CN106007209 discloses a pretreatment process for deoiling petroleum refining wastewater, which uses a combination of mechanical separation, coarse-grained treatment and air floatation technology to realize the pretreatment of oil and water separation.
  • the invention uses physical and chemical methods to work together and is pretreated
  • the oil content in the post-oily sewage is ⁇ 20mg / L, which meets the national standard, but the problem of VOCs generated by air flotation still exists.
  • FIG. 1 shows a flow chart of the conventional treatment process for oily sewage.
  • the oily sewage first enters the regulating tank 1 to achieve the preliminary separation of oil, mud and water in the regulating tank; the regulating tank effluent enters the grease trap 10 to further separate the oil, mud and water; the grease trap effluent enters Flotation tank 11 to remove dispersed oil and suspended particles; effluent from the flotation tank enters the A / O (anoxic / aerobic) biochemical tank 4 and uses microorganisms to remove organic matter in the wastewater; effluent from the biochemical tank enters the secondary sedimentation tank 12 for further deposition; The effluent from the secondary settling tank enters the advanced treatment equipment 5 for further processing to obtain purified water; among them, the sludge processed by the adjustment tank, grease trap and flotation tank is decoked, and the VOCs are depressurized by the gas system, and the treatment tank and grease trap are processed.
  • the oil deoiling recovery system In
  • the existing oily sewage treatment process the research on the method of reducing oil content is continuously deepened, but in the treatment process, the air floatation process is inevitably used.
  • the air floatation process can effectively remove dispersed oil and suspension and particulate matter It needs to be added to remove it.
  • the air floatation process often has the problems of large scum amount and volatile leakage of VOCs.
  • the present disclosure provides a novel method and device for eliminating air floatation of oily sewage pretreatment, thereby solving the problems in the prior art.
  • the present disclosure provides a method for pretreatment of oil-bearing sewage without air floatation.
  • the method includes the following steps:
  • Sedimentation separation Sedimentation separation of oily sewage to achieve the preliminary separation of oil, mud and water;
  • step (b) Fluidized bed separation: the oily sewage obtained by the preliminary separation in step (a) is subjected to fluidized bed separation to further remove the dispersed oil, mud and sand in the oily sewage;
  • step (c) Shape coalescence separation: shape coalescence separation of the oily sewage obtained by the fluidized bed separation in step (b) to achieve demulsification, coalescence and separation of emulsified oil;
  • step (d) Biochemical treatment: The effluent obtained in step (c) directly enters the biochemical system, eliminating the air floatation unit.
  • the method further includes: (e) advanced treatment: further processing the effluent obtained by the biochemical treatment in step (d); and (f) back-flushing of the ebullated bed: not more than per week The frequency of backflushing of the ebullated bed is once.
  • the steps (a) and (b) remove the suspended matter in the oily sewage, so that the concentration of suspended matter in the effluent drops to Below 50mg / L.
  • the steps (b) and (c) when the concentration of petroleum in the oily sewage is not higher than 20000 mg / L, the steps (b) and (c) remove oil, so that the concentration of petroleum falls below 20 mg / L; The residence time of oily sewage in steps (b) and (c) does not exceed 30 minutes in total.
  • the present disclosure provides an oil-bearing sewage pretreatment device that eliminates air floatation, and the device includes:
  • Adjusting tank used for sedimentation separation of oily sewage to achieve the preliminary separation of oil, mud and water;
  • the fluidized bed separator connected to the regulating tank is used for fluidized bed separation of the oily sewage obtained by preliminary separation to further remove the dispersed oil, mud and sand in the oily sewage;
  • a shape coalescer connected to the fluidized bed separator is used for shape coalescence separation of the oily sewage separated by the fluidized bed to achieve demulsification, coalescence and separation of emulsified oil;
  • the AOH Cosmetic Enhanced Anoxic / Aerobic biochemical tank connected to the shape coalescer is used to remove organic matter in the water out of the shape coalescing, in which the air flotation unit is eliminated.
  • the device further includes an advanced treatment device connected to the AOH biochemical tank for further advanced treatment of the effluent obtained by the biochemical treatment.
  • the bed packing of the fluidized bed separator is selected from filter materials with a particle size of 0.5-2mm; the top of the fluidized bed separator is equipped with one or more cyclone separators, In the backwashing process of the fluidized bed separator, the rotation of the particles in the cyclone separator is used to realize the regeneration of the filter material.
  • the shape coalescer adopts hydrophilic and oleophobic and lipophilic and hydrophobic modular internals of X, ⁇ -type fiber weaving method. In another preferred embodiment, the shape coalescer adopts oil-in-oil collection, automatic control, and intermittent oil discharge.
  • the pressure drop of the cascading shape coalescer set of the fluidized bed separator is not higher than 0.12MPa; compared with the traditional oil separation + flotation process, the floor space is saved by about 70%.
  • the invention adopts a combined process of sedimentation separation, ebullated bed separation and shape coalescence separation to realize the deoiling and desolidification of oily sewage, and eliminates the air flotation unit, thereby realizing no addition of chemicals, no air blowing and no flotation scum. It has the advantages of low cost, simple process and high separation efficiency.
  • Figure 1 shows a flow chart of the conventional treatment process for oily sewage.
  • FIG. 2 is a schematic diagram of a process for treating oily sewage according to an embodiment of the present invention.
  • Sedimentation separation can realize the preliminary separation of oil, mud and water
  • the fluidized bed separator can realize the deep filtration and the boiling swirl regeneration of the filter material
  • the shape coalescer can realize the demulsification, coalescence and separation of the emulsified oil
  • coalescer The effluent directly enters the biochemical pool, and the air floatation unit is eliminated.
  • a fluidized bed separator is used to perform fluidized bed separation on the oily sewage obtained in step (a) to further remove dispersed oil, mud and sand in the oily sewage;
  • Shape coalescence separation shape coalescence device is used to shape coalescence separation of the oily sewage obtained by the fluidized bed separation in step (b) to achieve demulsification, coalescence and separation of emulsified oil;
  • step (d) Biochemical treatment: The effluent obtained in step (c) directly enters the biochemical system, eliminating the air floatation unit.
  • the method further includes: (e) advanced treatment: the effluent obtained by the biochemical treatment in step (d) is further processed by using an AOH biochemical pool.
  • the method further includes: (f) Effluent bed backwashing: backflushing the ebullated bed separator at a frequency not higher than once a week.
  • the steps (a) and (b) can effectively remove the suspended matter in the oily sewage, so that the concentration of the suspended matter in the effluent drops to 50 mg / L below.
  • the steps (b) and (c) remove oil, so that the petroleum concentration drops below 20 mg / L.
  • the residence time of the oily sewage in the steps (b) and (c) does not exceed 30 minutes in total.
  • an air floatation-free oily sewage pretreatment device which includes:
  • Adjusting tank used for sedimentation separation of oily sewage to achieve the preliminary separation of oil, mud and water;
  • the fluidized bed separator connected to the regulating tank is used for fluidized bed separation of the oily sewage obtained by preliminary separation to further remove the dispersed oil, mud and sand in the oily sewage;
  • a shape coalescer connected to the fluidized bed separator is used for shape coalescence separation of the oily sewage separated by the fluidized bed to achieve demulsification, coalescence and separation of emulsified oil;
  • the AOH biochemical pool connected to the shape coalescer is used to remove the organic matter in the water from the shape coalescence, and the air float unit is eliminated.
  • the device further includes a deep treatment device connected to the AOH biochemical pool, which is used to further process the effluent obtained by the biochemical treatment.
  • the bed packing of the fluidized bed separator is selected from filter materials with a particle size of 0.5-2 mm.
  • the top of the ebullated bed separator is equipped with one or more cyclone separators.
  • the rotation and revolution of the particles in the cyclone separator are used to realize regeneration of the filter material.
  • the shape coalescer adopts hydrophilic and oleophobic and lipophilic and hydrophobic modular internals of X, ⁇ -type fiber weaving method.
  • the shape coalescer adopts oil-in-oil to collect oil, and adopts automatic control to intermittently discharge oil.
  • the pressure drop of the cascading shape coalescer set of the fluidized bed separator is not higher than 0.12 MPa; compared with the traditional oil separation + flotation process, the floor space is saved by about 70%.
  • FIG. 2 is a schematic diagram of a process for treating oily sewage according to an embodiment of the present invention.
  • the oily sewage first enters the regulating tank 1 to achieve the preliminary separation of oil, mud and water in the regulating tank; the effluent from the regulating tank enters the fluidized bed separator 2 to remove the dispersed oil, mud and sand in the oily sewage ;
  • the resulting oily sewage enters the shape coalescer 3 for further processing to achieve demulsification, coalescence and separation of emulsified oil (water-in-oil and oil-in-water);
  • the treated wastewater and air enter the AOH biochemical tank 4 for removal Organic matter in the wastewater; the effluent from the AOH biochemical tank enters the advanced treatment equipment 5 for further treatment to obtain purified water; after a period of operation, the fluidized bed separator is backwashed; where the sludge obtained from the treatment tank is decoked and the VOCs are depressurized Gas system, oil deo
  • This embodiment is applied to the pretreatment system of oily sewage in the refining area of a petrochemical refinery.
  • the existing pretreatment process of the sewage treatment plant at this base is a combined process of homogenization + oil separation + flotation. There is a risk that the cover is arranged in a tight manner.
  • the water quality conditions of the oily sewage used in this embodiment are shown in Table 1 below, and the treatment process flow is shown in FIG. 2.
  • the key equipment in the process is the fluidized bed separator and shape coalescer. In actual application, different numbers of equipment can be selected in parallel according to the different processing capacity.
  • the key equipment of the process is shell equipment, which is convenient for transportation and installation. In this embodiment, a fluidized oily sewage is treated with a fluidized bed separator coupled shape coalescer.
  • the pretreatment system is used to conduct continuous experiments on incoming water.
  • the experimental conditions are divided into normal conditions (oil content lower than 200mg / L) and impact conditions (oil content higher than 1000mg / L), and the influent and effluent conditions are determined.
  • the oil content and the measurement results are shown in Table 2 and Table 3 below.
  • the pretreatment system can effectively cope with the impact conditions of oily sewage. Under the impact conditions, it can recover more than 99% of the oil in the sewage, and at the same time effectively control the volatilization of VOCs, reducing the source The volatilization of VOCs.
  • the experimental results show that through the closed pretreatment process, more than 60% of the hydrocarbons in the oily sewage are prevented from leaking and diffusing in the traditional pretreatment unit. Instead, they are collected in a centralized manner in the form of hydrocarbons.
  • the fluidized bed separator can effectively intercept suspended solids and enrich and recover through regeneration. It is expected that the total amount of bottom sludge will be reduced by 30%, and the process of enrichment and recovery of bottom sludge will also achieve a closed circulation treatment.
  • the novel pretreatment method of the present invention has a stable effect of removing suspended solids and petroleum. It can be seen from the measurement results of the petroleum concentration of the inlet and outlet water that the petroleum concentration can be basically controlled below 30 mg / L under normal working conditions, removing most of the suspension The recovery efficiency of petroleum oil and emulsified oil reaches more than 99% under impact conditions, which has great economic benefits.
  • the pretreatment method can basically control the concentration of suspended matter below 50mg / L.

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Abstract

一种取消气浮的含油污水预处理方法，包括以下步骤：(a)沉降分离：对含油污水进行沉降分离，以实现油、泥、水的初步分离；(b)沸腾床分离：对步骤(a)中经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；(c)形状聚结分离：对步骤(b)中经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及(d)生化处理：步骤(c)中得到的出水直接进入AOH生化系统，取消气浮单元。还公开了一种取消气浮的含油污水预处理装置。

Description

取消气浮的含油污水预处理方法和装置 技术领域
本公开属于石油化工、环保领域，涉及一种含油污水处理技术。具体地说，本公开涉及沉降分离、沸腾床分离和形状聚结分离组合的含油污水处理方法。本公开还涉及一种含油污水处理装置。
背景技术
石油化工、环保、煤化工等领域存在大量含油污水的处理过程，废水中污染物种类较多，分别为油、悬浮物、细菌、溶解态有机物以及微量重金属元素。目前，针对含油污水，普遍采用隔油、浮选和生化的组合工艺。预处理工艺主要去除来水中的油份和悬浮物，是成套污水处理工艺的咽喉，预处理工艺的好坏直接影响生化单元处理的效果。
目前，含油污水预处理装置普遍存在的问题有：以1000m 3/h的含油污水处理规模，其隔油+浮选工艺药剂消耗如下：PAC(聚合氧化铝)年消耗6080t，FeCl 3年消耗2800t，PAM(聚丙烯酰胺)年消耗115t，药剂消耗巨大，成本较高，且易引起二次污染；浮选池需进行曝气，其VOCs(挥发性有机化合物)排放量可达8100Nm 3/h，运行过程中，构筑物结构较大，易导致VOCs泄漏；另外，浮选池的浮选浮渣产量在每月500t左右，产生大量含油危险废弃物。
针对含油污水中的主要污染物油和悬浮物，目前常用的处理方法是重力沉降、离心分离、吸附、以及气浮等方法，这些处理方法均有其使用的局限性，单独使用往往很难达到排放的要求。随着环保要求的逐渐提高，开发了一些方法的耦合工艺，国内外研究者已经做出了多方面的工作。
例如，美国专利申请US20120132588A1公开了一种含油废水的处理方法，以电化学絮凝和浮选作为预处理方法，并采用膜蒸馏的方法处理预处理出水，出水能够作为产生蒸汽的原水。但是该方法存在能耗较大的问题。
中国专利CN104843817B公开了一种水平气浮耦合波纹板除油方法及其装置，采用多层斜板单元与水平气浮耦合技术的优化组合方法，实现了三相的高效、迅速、低能耗的分离，适用于污水处理、原油开采等含油废水处理过程。
中国专利申请CN106007209公开了一种石油炼油污水除油预处理工艺，利用 机械分离、粗粒化处理以及气浮技术组合实现油水分离的预处理，该发明采用物理和化学方法共同作用，经预处理后含油污水中含油量≤20mg/L，达到国家标准，但是依然存在气浮产生VOCs的问题。
图1示出了含油污水的传统处理工艺流程图。如图1所示，含油污水首先进入调节罐1，在调节罐中实现油、泥、水的初步分离；调节罐出水进入隔油池10，进一步分离油、泥、水；隔油池出水进入浮选池11，去除分散油和悬浮颗粒物；浮选池出水进入A/O(缺氧/好氧)生化池4，利用微生物去除废水中的有机物；生化池出水进入二沉池12进一步沉积；二沉池出水进入深度处理设备5做进一步处理，得到净化水；其中，调节罐、隔油池和浮选池处理得到的油泥去焦化，VOCs去低压瓦斯系统，调节罐和隔油池处理得到的油去油回收系统，二沉池沉降的活性污泥部分返回生化池继续处理，部分去剩余污泥处理系统。
现有的含油污水处理工艺，针对降低油含量方法上的研究正不断深入，但在处理工艺中不可避免地使用了气浮工艺，气浮工艺能够有效去除分散油和悬浮和颗粒物，对乳化油则需要添加药剂加以去除。另外，气浮工艺往往存在着浮渣量较大以及VOCs挥发泄露等问题。
因此，本领域迫切需要开发一种短流程、能够实现VOCs减排和油泥减量，克服了现有技术中上述气浮工艺的缺陷的方法和装置。
发明内容
本公开提供了一种新颖的取消气浮的含油污水预处理方法和装置，从而解决了现有技术中存在的问题。
一方面，本公开提供了一种取消气浮的含油污水预处理方法，该方法包括以下步骤：
(a)沉降分离：对含油污水进行沉降分离，以实现油、泥、水的初步分离；
(b)沸腾床分离：对步骤(a)中经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；
(c)形状聚结分离：对步骤(b)中经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
(d)生化处理：步骤(c)中得到的出水直接进入生化系统，取消气浮单元。
在一个优选的实施方式中，该方法还包括：(e)深度处理：对步骤(d)中经 生化处理得到的出水进一步进行处理；以及(f)沸腾床反冲洗：以不高于每周一次的频率对沸腾床进行反冲洗。
在另一个优选的实施方式中，当含油污水中悬浮物浓度不高于5000mg/L时，所述步骤(a)和步骤(b)去除含油污水中的悬浮物，使得出水悬浮物浓度降至50mg/L以下。
在另一个优选的实施方式中，当含油污水中石油类浓度不高于20000mg/L时，所述步骤(b)和步骤(c)除油，使得石油类浓度降至20mg/L以下；所述步骤(b)和步骤(c)中含油污水的停留时间总共不超过30分钟。
另一方面，本公开提供了一种取消气浮的含油污水预处理装置，该装置包括：
调节罐，用于对含油污水进行沉降分离，以实现油、泥、水的初步分离；
与调节罐连接的沸腾床分离器，用于对经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；
与沸腾床分离器连接的形状聚结器，用于对经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
与形状聚结器连接的AOH(旋流强化缺氧/好氧)生化池，用于去除形状聚结出水中的有机物，其中，取消了气浮单元。
在一个优选的实施方式中，该装置还包括与AOH生化池连接的深度处理设备，用于对经生化处理得到的出水进一步深度处理。
在另一个优选的实施方式中，所述沸腾床分离器的床层填料选用粒径在0.5-2mm的滤料；所述沸腾床分离器的顶部装有一个或多个旋流分离器，在沸腾床分离器的反冲洗过程中利用旋流分离器中颗粒自转实现滤料再生。
在另一个优选的实施方式中，所述形状聚结器采用X、Ω型纤维编制方法的亲水疏油和亲油疏水的模块化内件。在另一个优选的实施方式中，所述形状聚结器采用油包集油，采用自动控制，间歇性排油。
在另一个优选的实施方式中，所述沸腾床分离器串联形状聚结器成套装置的压降不高于0.12MPa；相比传统隔油+浮选工艺，占地面积节省约70％。
有益效果：
本发明的方法和装置的主要优点在于：
本发明采用沉降分离、沸腾床分离和形状聚结分离组合的工艺实现含油污水 的除油脱固，并取消了气浮单元，实现了不加药剂、不鼓空气和不产生浮选浮渣，具有成本低廉、流程简单、分离效率高等优点。
附图说明
附图是用以提供对本公开的进一步理解的，它只是构成本说明书的一部分以进一步解释本公开，并不构成对本公开的限制。
图1示出了含油污水的传统处理工艺流程图。
图2是根据本发明一个实施方式的含油污水处理的工艺示意图。
具体实施方式
本申请的发明人经过广泛而深入的研究后发现，对于含油污水这种操作通量大，含固相、水相和油相的混合体系，常用的预处理方法是均质、隔油和浮选的组合工艺，但是这些常规工艺存在流程复杂、操作弹性小等问题，因此，发明了沉降分离、沸腾床分离和形状聚结分离组合的预处理工艺对含油污水除油和悬浮物，其中，沉降分离可实现油、泥、水的初步分离，沸腾床分离器可实现深层过滤和滤料的沸腾旋流再生，形状聚结器可实现乳化油的破乳、聚结和分离；聚结器出水直接进入生化池，取消气浮单元。基于上述发现，本发明得以完成。
在本公开的第一方面，提供了一种取消气浮的含油污水预处理方法，该方法包括以下步骤：
(a)沉降分离：在调节罐中对含油污水进行沉降分离，以实现油、泥、水的初步分离；
(b)沸腾床分离：采用沸腾床分离器对步骤(a)中经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂等；
(c)形状聚结分离：采用形状聚结器对步骤(b)中经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
(d)生化处理：步骤(c)中得到的出水直接进入生化系统，取消气浮单元。
在本公开中，该方法还包括：(e)深度处理：采用AOH生化池对步骤(d)中经生化处理得到的出水进一步进行处理。
在本公开中，该方法还包括：(f)沸腾床反冲洗：以不高于每周一次的频率 对沸腾床分离器进行反冲洗。
在本公开中，当含油污水中悬浮物浓度不高于5000mg/L时，所述步骤(a)和步骤(b)能够有效地去除含油污水中的悬浮物，使得出水悬浮物浓度降至50mg/L以下。
在本公开中，当含油污水中石油类浓度不高于20000mg/L时，所述步骤(b)和步骤(c)除油，使得石油类浓度降至20mg/L以下。
在本公开中，所述步骤(b)和步骤(c)中含油污水的停留时间总共不超过30分钟。
在本公开的第二方面，提供了一种取消气浮的含油污水预处理装置，该装置包括：
调节罐，用于对含油污水进行沉降分离，以实现油、泥、水的初步分离；
与调节罐连接的沸腾床分离器，用于对经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；
与沸腾床分离器连接的形状聚结器，用于对经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
与形状聚结器连接的AOH生化池，用于去除形状聚结出水中的有机物，其中，取消了气浮单元。
在本公开中，该装置还包括与AOH生化池连接的深度处理设备，用于对经生化处理得到的出水进一步进行处理。
在本公开中，所述沸腾床分离器的床层填料选用粒径在0.5-2mm的滤料。
在本公开中，所述沸腾床分离器的顶部装有一个或多个旋流分离器，在沸腾床分离器的反冲洗过程中利用旋流分离器中颗粒自转与公转实现滤料再生。
在本公开中，所述形状聚结器采用X、Ω型纤维编制方法的亲水疏油和亲油疏水的模块化内件。
在本公开中，所述形状聚结器采用油包集油，并采用自动控制，间歇排油。
在本公开中，所述沸腾床分离器串联形状聚结器成套装置的压降不高于0.12MPa；相比传统隔油+浮选工艺，占地面积节省约70％。
以下参看附图。
图2是根据本发明一个实施方式的含油污水处理的工艺示意图。如图2所示， 含油污水首先进入调节罐1，在调节罐中实现油、泥、水的初步分离；调节罐出水进入沸腾床分离器2，去除含油污水中的分散油、泥和砂等；所得含油污水进入形状聚结器3进一步处理，实现对乳化油(油包水和水包油)的破乳、聚结和分离；经过处理后的废水连同空气进入AOH生化池4，以去除废水中的有机物；AOH生化池出水进入深度处理设备5做进一步处理，得到净化水；运行一段时间后，对沸腾床分离器进行反冲洗；其中，调节罐处理得到的油泥去焦化，VOCs去低压瓦斯系统，油去油回收系统；沸腾床分离器的顶部装有一个或多个旋流分离器6，以在沸腾床分离器的反冲洗过程中利用旋流分离器中颗粒自转与公转实现滤料再生，旋流分离器溢流返回调节罐继续处理；形状聚结器利用除油模块实现油水分离，并通过油包7集油，分离得到的油去油回收系统；AOH生化池利用活性污泥进一步处理聚结器出水，二沉池沉降的活性污泥部分返回生化池循环利用，部分去剩余污泥处理系统。
实施例
下面结合具体的实施例进一步阐述本发明。但是，应该明白，这些实施例仅用于说明本发明而不构成对本发明范围的限制。下列实施例中未注明具体条件的试验方法，通常按照常规条件，或按照制造厂商所建议的条件。除非另有说明，所有的百分比和份数按重量计。
实施例1：
1.工艺流程
本实施例应用于某石化炼厂炼油区含油污水预处理系统中，该基地现有污水处理厂预处理工艺为均质+隔油+浮选组合工艺，工艺流程相对较长，且相应构筑物加盖的布置方式存在密闭不严的风险。本实施例中所用含油污水水质条件如下表1，其处理工艺流程如图2所示。
2.关键设备
该工艺流程中的关键设备为沸腾床分离器和形状聚结器，在实际应用中，可根据处理量的不同选择并联不同数量的设备，工艺关键设备均为壳装设备，便于运输安装。本实施例中采用沸腾床分离器耦合形状聚结器处理石化含油污水。
3.运行效果
含油污水水质条件见下表1：
表1：来水水质条件
Figure PCTCN2019078618-appb-000001
采用预处理系统对来水进行连续实验，实验工况分为常规工况(油含量低于200mg/L)和冲击工况(油含量高于1000mg/L)，并测定其进水和出水的油含量，测定结果如下表2和表3所示。
表2：常规工况下进出水油含量
时间 进水油含量(mg/L) 出水油含量(mg/L)
第1天 98.2 33.8
第2天 125 28.5
第3天 76.9 29.4
第4天 47.2 21.3
第5天 44.9 25.3
表3：冲击工况下进出水油含量
时间 进水油含量(mg/L) 出水油含量(mg/L)
第1天 15000 41.1
第2天 10000 42.2
第3天 5000 59.1
第5天 10000 55.3
第6天 20000 65.2
通过进出水水质分析看出，该预处理系统能有效应对含油污水冲击工况，在冲击工况下，能够回收污水中99％以上的油，同时有效控制了VOCs的挥发，从源头上减少了VOCs的挥发。实验结果表明，通过密闭预处理工艺，避免了含油污水中60％以上的烃类在传统预处理单元中的泄漏和扩散，而是通过烃类形式被分类集中收集。另外，本实施例中，沸腾床分离器能够有效拦截悬浮物，并通过再生方式富集回收，预期使底泥总量减少30％，且底泥富集回收过程也实现了循环密闭处理。
本发明的新型预处理方法脱除悬浮物和石油类效果稳定，通过进出水石油类浓度测定结果可以看出，常规工况下石油类浓度基本能够控制在30mg/L以下，去除了大多数悬浮态油和乳化油，冲击工况下，石油类回收效率达到99％以上，具有较大的经济效益；另外，该预处理方法能够将悬浮物浓度基本控制在50mg/L以下。
上述所列的实施例仅仅是本公开的较佳实施例，并非用来限定本公开的实施范围。即凡依据本申请专利范围的内容所作的等效变化和修饰，都应为本公开的技术范畴。
在本公开提及的所有文献都在本申请中引用作为参考，就如同每一篇文献被单独引用作为参考那样。此外应理解，在阅读了本公开的上述讲授内容之后，本领域技术人员可以对本公开作各种改动或修改，这些等价形式同样落于本申请所附权利要求书所限定的范围。

Claims (10)

  1. 一种取消气浮的含油污水预处理方法，该方法包括以下步骤：
    (a)沉降分离：对含油污水进行沉降分离，以实现油、泥、水的初步分离；
    (b)沸腾床分离：对步骤(a)中经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；
    (c)形状聚结分离：对步骤(b)中经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
    (d)生化处理：步骤(c)中得到的出水直接进入生化系统，取消气浮单元。
  2. 如权利要求1所述的方法，其特征在于，该方法还包括：(e)深度处理：对步骤(d)中经生化处理得到的出水进一步进行处理；以及(f)沸腾床反冲洗：以不高于每周一次的频率对沸腾床进行反冲洗。
  3. 如权利要求1或2所述的方法，其特征在于，当含油污水中悬浮物浓度不高于5000mg/L时，所述步骤(a)和步骤(b)去除含油污水中的悬浮物，使得出水悬浮物浓度降至50mg/L以下。
  4. 如权利要求1或2所述的方法，其特征在于，当含油污水中石油类浓度不高于20000mg/L时，所述步骤(b)和步骤(c)除油，使得石油类浓度降至20mg/L以下；所述步骤(b)和步骤(c)中含油污水的停留时间总共不超过30分钟。
  5. 一种取消气浮的含油污水预处理装置，该装置包括：
    调节罐(1)，用于对含油污水进行沉降分离，以实现油、泥、水的初步分离；
    与调节罐(1)连接的沸腾床分离器(2)，用于对经初步分离得到的含油污水进行沸腾床分离，以进一步去除含油污水中的分散油、泥和砂；
    与沸腾床分离器(2)连接的形状聚结器(3)，用于对经沸腾床分离得到的含油污水进行形状聚结分离，以实现乳化油的破乳、聚结和分离；以及
    与形状聚结器(3)连接的AOH生化池(4)，用于去除形状聚结出水中的有机物，其中，取消了气浮单元。
  6. 如权利要求5所述的装置，其特征在于，该装置还包括与AOH生化池(4)连接的深度处理设备(5)，用于对经生化处理得到的出水进一步进行处理。
  7. 如权利要求5或6所述的装置，其特征在于，所述沸腾床分离器(2)的床层填料选用粒径在0.5-2mm的滤料；所述沸腾床分离器(2)的顶部装有一个或 多个旋流分离器(6)，在沸腾床分离器(2)的反冲洗过程中利用旋流分离器(6)中颗粒自转实现滤料再生。
  8. 如权利要求5或6所述的装置，其特征在于，所述形状聚结器(3)采用X、Ω型纤维编制方法的亲水疏油和亲油疏水的模块化内件。
  9. 如权利要求5或6所述的装置，其特征在于，所述形状聚结器(3)采用油包(7)集油，并采用自动控制，间歇性排油。
  10. 如权利要求5或6所述的装置，其特征在于，所述沸腾床分离器(2)串联形状聚结器(3)成套装置的压降不高于0.12MPa；相比传统隔油+浮选工艺，占地面积节省70％。
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