WO2022241869A1 - 油田采出水的处理方法和处理装置 - Google Patents

油田采出水的处理方法和处理装置 Download PDF

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WO2022241869A1
WO2022241869A1 PCT/CN2021/098650 CN2021098650W WO2022241869A1 WO 2022241869 A1 WO2022241869 A1 WO 2022241869A1 CN 2021098650 W CN2021098650 W CN 2021098650W WO 2022241869 A1 WO2022241869 A1 WO 2022241869A1
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produced water
oilfield produced
water
oilfield
treatment
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PCT/CN2021/098650
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English (en)
French (fr)
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胡以朋
梁仁刚
郝晋伟
尹啊慧
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杰瑞环保科技有限公司
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Publication of WO2022241869A1 publication Critical patent/WO2022241869A1/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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • 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
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • C02F1/60—Silicon compounds
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • 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
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/026—Fenton's reagent
    • 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
    • C02F3/02—Aerobic processes
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/104—Granular carriers
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/105—Characterized by the chemical composition
    • C02F3/106—Carbonaceous materials
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/105—Characterized by the chemical composition
    • C02F3/107—Inorganic materials, e.g. sand, silicates
    • 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
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C02F5/06—Softening water by precipitation of the hardness using calcium compounds

Definitions

  • Embodiments of the present disclosure relate to a method for treating oilfield produced water and a treatment device for oilfield produced water.
  • Heavy oil thermal recovery is currently the most effective and widely used method for enhancing heavy oil recovery.
  • Heavy oil thermal recovery mainly includes steam huff and puff, steam drive, and steam-assisted gravity drainage.
  • steam huff and puff In the process of thermal recovery of heavy oil, it is necessary to continuously add high-temperature and high-pressure steam to the formation to reduce the viscosity of crude oil, and this process consumes a lot of fresh water and heat energy.
  • Heavy oil produced water has the characteristics of high salinity, high temperature, high hardness, easy formation of oil-in-water emulsion, small oil-water density difference, high silicon content, and high pollutant content.
  • a large amount of surplus sewage is ineffectively recharged, and the ecology of the area where the heavy oil reservoir is located is fragile. If the heavy oil production water is directly discharged into the external environment, it will not only damage the ecological environment, but also cause water pollution. The waste of resources has caused a great negative impact on the oilfield water balance.
  • the oilfield production situation is becoming more and more severe, and clean water resources are increasingly scarce. Treating excess heavy oil produced water to a reusable standard is of great significance to the oilfield's ecological and environmental protection, and can also save water resources.
  • At least one embodiment of the present disclosure provides a method for treating oilfield produced water, the method comprising: providing oilfield produced water; cooling and purifying the oilfield produced water to obtain produced water; combining the subsequent oilfield produced water with the The produced water is heat exchanged to lower the temperature of the subsequent oilfield produced water and to increase the temperature of the produced water.
  • exchanging heat between the oilfield produced water and the produced water includes: using a heat exchange component to perform the heat exchange, so as to reduce the temperature of the oilfield produced water , and increase the temperature of the product water.
  • after performing the heat exchange by using a heat exchange component further include: using a radiator to dissipate heat.
  • the method after performing the heat exchange, it further includes: using a cooling tower to lower the temperature of the oilfield produced water again, so that the temperature of the oilfield produced water is lower than 35 °C.
  • purifying the oilfield produced water includes: oxidizing the oilfield produced water that has undergone the cooling treatment using an oxidation tank to decompose the oilfield produced water at least part of the organic matter.
  • purifying the oilfield produced water includes: using a biological aerated filter to decompose and/or mineralize the oilfield produced water to remove the organic matter .
  • the filler before using the biological aerated filter to decompose and/or mineralize the oilfield produced water, it also includes: The filler is activated, wherein the activation of the filler in the biological aerated filter includes: flushing the biological aerated filter with clean water to remove impurities adsorbed by the filler and/or the filler is The powder produced by abrasion; the filler is treated with sodium hydroxide solution to remove the organic impurities contained in the filler, and the filler is treated with water to neutrality; the filler is treated with sulfuric acid solution to remove the adsorption of the filler Inorganic matter, and use clean water to treat the filler to neutrality.
  • the filler in the biological aerated filter includes at least one of coconut shell charcoal, almond shell charcoal and coal-based activated carbon.
  • the method provided in at least one embodiment of the present disclosure further includes: adding a salt-tolerant bacteria agent into the biological aerated filter, wherein the quality of the salt-tolerant bacteria agent per cubic meter of the oilfield produced water is 5-50 g, and the number of effective bacteria in the salt-tolerant bacteria agent per gram of the oilfield produced water is greater than or equal to 200 million.
  • the method provided in at least one embodiment of the present disclosure further includes: performing ultrafiltration treatment on the effluent of the biological aerated filter by using an ultrafiltration element.
  • the method provided in at least one embodiment of the present disclosure further includes: using a reverse osmosis element to perform reverse osmosis treatment on the effluent of the ultrafiltration element to perform desalination.
  • the method provided in at least one embodiment of the present disclosure further includes: using a resin filter to treat the concentrated water after the reverse osmosis treatment, wherein the produced water is output from the resin filter.
  • the pretreatment includes: using a regulating tank At least one of a nitrogen air flotation unit, a hard and silicon removal unit, a sedimentation tank and a filter unit is used to treat the oilfield produced water.
  • At least one embodiment of the present disclosure also provides a treatment device for oilfield produced water, including: an oilfield produced water supply component configured to provide oilfield produced water; a heat exchange component configured to cool down the oilfield produced water; a purification component , configured to purify the oilfield produced water after the cooling treatment to obtain produced water; the water delivery pipe is configured to transport the produced water, wherein the first end of the heat exchange component is connected to the oilfield produced water supply component The second end of the heat exchange component is connected to the water delivery pipe, so that the oilfield produced water and the produced water perform heat exchange in the heat exchange component to cool down the oilfield produced water .
  • the heat exchange component includes a heat exchanger.
  • the processing device provided in at least one embodiment of the present disclosure further includes a radiator, wherein the radiator is configured to dissipate heat from the oilfield produced water.
  • the treatment device provided in at least one embodiment of the present disclosure further includes a cooling tower, wherein the cooling tower is arranged between the heat exchange component and the purification component.
  • the purification component includes at least one of an oxidation pond, a biological aerated filter, an ultrafiltration element, a reverse osmosis element, and a resin filter.
  • the oxidation cell includes an electrocatalytic oxidation component, or a combination of ozone and hydrogen peroxide, or an electrocatalytic oxidation component, and a combination of ozone and hydrogen peroxide.
  • the filler in the biological aerated filter is at least one of coconut shell charcoal, almond shell charcoal and coal-based activated carbon.
  • the treatment device provided in at least one embodiment of the present disclosure further includes a pretreatment unit, wherein the pretreatment unit includes at least one of a regulating tank, a nitrogen air flotation unit, a hard and silicon removal unit, a sedimentation tank, and a filtration unit one.
  • the pretreatment unit includes at least one of a regulating tank, a nitrogen air flotation unit, a hard and silicon removal unit, a sedimentation tank, and a filtration unit one.
  • the filter unit includes a membrane-coated fiber ball filter and a tubular microfiltration membrane filter.
  • Fig. 1 is a flowchart of a treatment method for oilfield produced water provided by an embodiment of the present disclosure
  • Fig. 2 is a process diagram of a treatment method for oilfield produced water provided by an embodiment of the present disclosure
  • FIG. 3 is a flowchart of a pretreatment section provided by an embodiment of the present disclosure
  • Fig. 4 is a flowchart of a treatment method for oilfield produced water provided by an embodiment of the present disclosure
  • FIG. 5 is a schematic diagram of the connection structure of a treatment device for oilfield produced water provided by an embodiment of the present disclosure
  • Fig. 6 is a schematic diagram of the connection structure of another treatment device for oilfield produced water provided by an embodiment of the present disclosure.
  • Fig. 7 is a schematic structural diagram of forming nitrogen air flotation provided by an embodiment of the present disclosure.
  • Steam injection boiler water has high requirements on salt content.
  • the treatment technologies for oilfield produced water reuse as steam injection boiler water mainly include thermal treatment and membrane treatment.
  • Thermal treatment technology uses evaporation and desalination to recover distilled water, and the equipment used includes mechanical vapor recompression (MVR), mechanical vapor compressor (MVC) or multi-effect evaporator. In this way, more than 80% of high-quality distilled water can be recovered.
  • MVR mechanical vapor recompression
  • MVC mechanical vapor compressor
  • multi-effect evaporator multi-effect evaporator.
  • the recovery rate of distilled water is related to the salt content in oilfield produced water. The higher the concentration of salt in the treated oilfield produced water, the higher the energy required for evaporation, the higher the latent heat of vaporization of water, and the water changes from liquid to gas The higher the energy required for the phase transition to occur.
  • the instant heat treatment technology needs to consume a lot of steam heating or electric energy to raise the temperature, the treatment cost is high, and the equipment used is bulky.
  • oilfield produced water usually has high chlorine content and high salt content.
  • the material requirements for high-temperature evaporation devices are extremely high, resulting in high equipment investment and operating costs for thermal treatment technology.
  • Membrane treatment technology is significantly lower than thermal treatment technology in terms of treatment cost and equipment investment.
  • the main equipment used in membrane treatment technology includes ultrafiltration membrane (UF), nanofiltration membrane (NF) and reverse osmosis membrane (RO) etc.
  • UF ultrafiltration membrane
  • NF nanofiltration membrane
  • RO reverse osmosis membrane
  • the limit temperature of these membrane modules is 45°C. Therefore, when the oilfield produced water is treated at a higher temperature, these membrane modules will be damaged.
  • Oilfield produced water for example, the temperature of heavy oil produced water is basically around 70°C. Therefore, it is necessary to lower the temperature of oilfield produced water to below 35-45°C first, and then treat
  • the inventors of the present disclosure have noticed that the current membrane treatment method only has the process of heat dissipation and cooling, and the heat energy cannot be recycled.
  • the process of reducing the temperature of the oilfield produced water from about 70°C to 35-45°C this part
  • the thermal energy is recycled, that is, the heat exchange between the high-temperature oilfield produced water to be treated and the clean produced water obtained from the treated oilfield produced water is realized.
  • the cooling also realizes the reuse of waste heat, thereby realizing energy saving and emission reduction.
  • At least one embodiment of the present disclosure provides a method for treating oilfield produced water, the method comprising: providing oilfield produced water; cooling and purifying the oilfield produced water to obtain produced water; heat-processing the subsequent oilfield produced water and produced water Exchange to reduce the temperature of the subsequent oilfield produced water and increase the temperature of the produced water.
  • FIG. 1 is a flow chart of a method for treating oilfield produced water provided by an embodiment of the present disclosure, including the following steps:
  • Step S01 providing oilfield produced water.
  • the oilfield produced water is heavy oil produced water.
  • thermal recovery boilers to inject steam, that is, to continuously add high-temperature and high-pressure steam to the formation to reduce the viscosity of crude oil. Therefore, the temperature of untreated heavy oil production water is usually around 70°C.
  • Heavy oil produced water has the characteristics of high production fluid viscosity, large sand carrying capacity, high hardness and high salinity.
  • Step S02 cooling and purifying the oilfield produced water to obtain produced water.
  • Step S03 Perform heat exchange between the subsequent oilfield produced water and produced water, so as to reduce the temperature of the subsequent oilfield produced water and increase the temperature of produced water.
  • steam injection boiler water has high requirements on salt content, so it can only be clean water, and needs to have a certain temperature. Therefore, the produced water after the temperature rise can be reused as gas injection boiler water.
  • exchanging heat between oilfield produced water and produced water includes: using heat exchange components for heat exchange, so that the temperature of oilfield produced water is lowered and the temperature of produced water is increased.
  • the first end of the heat exchange component is connected to the pipe fitting for the input of oilfield produced water, and the second end of the heat exchange component is connected to the water delivery pipe for transmitting the produced water.
  • the oilfield produced water and produced water flow in reverse, so that the oilfield produced water and produced water
  • the water performs heat exchange in the heat exchange components to cool down the oilfield produced water and increase the temperature of the produced water for use as gas injection boiler water.
  • the heat exchange component includes a spiral plate heat exchanger or a plate heat exchanger, and the heat exchange component includes a high-efficiency plate heat exchange device, and the high-efficiency plate heat exchange device is detachable to facilitate installation and transportation.
  • the high-efficiency plate heat exchange equipment is, for example, formed of titanium alloy material, such as titanium steel alloy, so that the high-efficiency plate heat exchange equipment can withstand a temperature of 500-550°C.
  • FIG. 2 is a process diagram of a treatment method for oilfield produced water provided by an embodiment of the present disclosure. As shown in FIG. 2 , after heat exchange is performed using heat exchange components, it further includes: using a radiator to dissipate heat.
  • radiators can be used to further reduce the temperature of oilfield produced water to reduce the risk of subsequent damage to ultrafiltration membranes (UF), nanofiltration membranes (NF) and reverse osmosis membranes (RO).
  • UF ultrafiltration membranes
  • NF nanofiltration membranes
  • RO reverse osmosis membranes
  • the heat exchange components Combined with the radiator, it can reduce the load of the radiator and equipment investment, that is, compared with the situation of directly using the radiator to dissipate heat without using heat exchange components, it can reduce the load of the radiator and make the radiator Lifespan is not shortened.
  • the treatment method may also include: using a cooling tower to cool down the oilfield produced water again, so that the temperature of the oilfield produced water is lower than 35°C, so that the temperature is lower than 35°C.
  • UF ultrafiltration membrane
  • NF nanofiltration membrane
  • RO reverse osmosis membrane
  • the cooling tower is a closed cooling tower, and the cooling tower uses water as a circulating coolant, and the circulating coolant and oilfield produced water are located in different pipelines, and the circulating coolant absorbs heat from the oilfield produced water to reduce oilfield The temperature of the produced water, and then the circulating coolant discharges the heat to the atmosphere to lower the temperature of the circulating cooling water.
  • the cooling tower is directly connected to the radiator to further reduce the temperature of the oilfield produced water, and the cooling tower is cooled by cold air.
  • the purification treatment of oilfield produced water includes: oxidizing the cooled oilfield produced water with an oxidation pond to decompose at least part of the organic matter in the oilfield produced water.
  • oxidation using an oxidation tank includes oxidation with ozone and hydrogen peroxide, or oxidation with electrocatalysis, or a combination of oxidation with ozone and hydrogen peroxide and oxidation with electrocatalysis.
  • Fenton oxidation may be included, which is not limited by embodiments of the present disclosure.
  • decomposing at least part of the organic matter in the oilfield produced water includes using an oxidation pond to decompose the emulsified and dissolved organic matter in the oilfield produced water, reducing the fouling of the macromolecular organic matter in the oilfield produced water to the subsequent membrane system, and at the same time improving the oilfield produced water. biodegradability.
  • COD chemical oxygen demand
  • oilfield produced water is still high, about 400-600 mg/L.
  • High chemical oxygen demand (COD) is easy to cause fouling of the membrane treatment system, and organic pollutants are not easy to backwash, and the membrane flux is not easy to recover after a decrease.
  • the concentration of ozone in the oxidation pool is 5-30 mg/L, and the oxidation time in the oxidation pool is less than or equal to 10 minutes.
  • the COD (chemical oxygen demand) of the produced water is less than 45mg/L.
  • ozone thermal oxidation can greatly improve the treatment effect of ozone on refractory organic matter in oilfield produced water.
  • an oxidation pond is added on the basis of conventional pretreatment, and the oxidation pond can decompose dissolved and emulsified organic matter in oil field production water, thereby reducing fouling of membrane equipment.
  • the oilfield produced water treated in the oxidation tank enters the biochemical treatment unit to deeply mineralize the organic matter, so that the impact of the organic matter on the membrane flux can be further reduced.
  • the oxidation tank treatment method can be directly used in the treatment of oilfield produced water, which can not only ensure the treatment effect of oilfield produced water, but also greatly reduce the treatment cost.
  • the whole process is simple and operable.
  • oilfield produced water is treated in an oxidation pond and then enters a biochemical treatment unit, which can deeply mineralize organic matter to further reduce the impact of organic matter on membrane flux.
  • purifying oilfield produced water includes: using a biological aerated filter (BAF) to perform at least one of decomposing and mineralizing oilfield produced water to remove organic matter.
  • BAF biological aerated filter
  • plastic honeycomb packing is installed in the biological aerated filter, and the packing is submerged in water, and a blower is used to aerate and oxygenate the bottom of the packing for blast aeration.
  • the air can entrain the oilfield produced water to be treated from bottom to top, and freely pass through the filter material to reach the ground. After the air escapes, the aerated biological filter will return to the bottom of the aerated biological filter from top to bottom at the filter material interval. .
  • the active cuttings are attached to the surface of the filler and do not flow with the water.
  • the biofilm is directly renewed by the strong agitation of the updraft, and the purification effect has been greatly improved.
  • the aerobic treatment process adopts contact oxidation biofilm technology, which can significantly remove dissolved organic pollutants and colloidal organic pollutants in oilfield produced water.
  • the biological aerated filter uses the loaded granular filler as the carrier, the granular filler and the attached biofilm as the main treatment medium, and fully exerts biological metabolism, biological flocculation, physical filtration, and membrane and filler Physical adsorption and interception to achieve efficient removal of organic pollutants.
  • a biological aerated filter can serve the purpose of filtering suspended solids and reducing the concentration of biodegradable substances.
  • a biological aerated filter is composed of a tank body, a filter material, a supporting layer, a water distribution system, a backwash system, a water outlet system, and an automatic control system;
  • the body of a biological aerated filter can be a conventional reactor , Fillers can be used in the reactor, and the scale of the biological aerated filter can be determined according to the amount of circulating water and the concentration of pollutants in the circulating water.
  • corresponding control systems, power systems and monitoring systems can also be set up according to needs.
  • the use of biological aerated filter to decompose and mineralize oilfield produced water is one of the main methods for deep removal of organic pollutants.
  • Traditional biochemical tanks occupy a large area and the membrane-hanging period is as long as 30 to 40 days , large amount of aeration, high cost of use.
  • the biological aerated filter is used to replace the traditional biochemical tank, which integrates biological oxidation, biological flocculation and filtration, and does not need to set up a secondary sedimentation tank, which not only meets the biochemical requirements, but also achieves the purpose of reducing the floor area and infrastructure investment.
  • the oxygen transmission efficiency in the biological aerated filter is high, the aeration volume is small, the power consumption of oxygen supply is low, the power consumption of the unit oilfield produced water is low, the degree of automation is high, the operation and management are convenient, and the membrane hanging cycle can be shortened to 14 ⁇ 21 days.
  • the operating time of the biological aerated filter is 24h-72h, such as 24h, 36h, 48h or 72h.
  • the biological aerated filter needs to be backwashed, and the backwashing adopts air-water linkage operation.
  • the total backwashing time is 1 hour, including 0.5 hours of backwashing time and 0.5 hours of recovery time.
  • the backwashing wind of the internal circulation biological aerated filter adopts non-purifying wind, the backwashing wind pressure is greater than 0.45MPa, and the backwashing air volume is 2-3 times of the treated water volume.
  • the backwash water is the supernatant of the backwash sedimentation tank, and the amount of backwash water is 1.6-2.0 times the amount of treated water.
  • the backwash drainage enters the backwash sedimentation tank for mud-water separation, and after static sedimentation, the supernatant is used as backwash water for the next backwash.
  • activating the filler in the biological aerated filter before using the biological aerated filter to decompose and/or mineralize the oilfield produced water, it also includes: activating the filler in the biological aerated filter , wherein, activating the filler in the biological aerated filter includes: washing the biological aerated filter with clean water, removing at least one of the impurities adsorbed by the filler and the powder produced by the wear of the filler, using sodium hydroxide
  • the filler is treated with solution to remove the organic impurities contained in the filler, and the filler is treated with water to neutrality, and then the filler is treated with sulfuric acid solution to remove the inorganic substances adsorbed by the filler, and the filler is treated with water to neutrality.
  • the fillers in the conventional biological aerated filter are used directly, and the fillers will be polluted by dust, clay, grease, etc. during the process of processing, transporting and packaging the fillers.
  • the current processing technology causes the microscopic voids inside the filler to be unsmooth or clogged to a certain extent, which makes the adsorption effect of the filter material worse, and the effective specific surface is reduced, thereby affecting the film-hanging cycle.
  • the activation process after filling the filler includes: flushing the biological aerated filter with clean water to remove impurities adsorbed by the filler and/or powder produced by the filler being worn; treating the filler with sodium hydroxide solution to remove the organic impurities contained in the filler , and use clean water to treat the filler to neutral; use sulfuric acid solution to treat the filler to remove the inorganic substances adsorbed by the filler, and use clean water to treat the filler to neutral.
  • the specific activation process after filling the packing includes: the first step is to rinse with clean water 2 to 3 times to wash away the impurities adsorbed by the filter material and the invalid powder produced by the wear of the filter material; the second step is to use 5 Wash and soak the filler with 5% sodium hydroxide for 4 hours to remove the grease and organic matter on the surface of the filler; after emptying the sodium hydroxide lye, rinse it with water until neutral; the third step, use 5% sulfuric acid to wash and soak for 4 hours, acidify and clean The throat void of the filler dissolves the impurities adsorbed inside and outside the filler.
  • the activation process can improve the film-hanging ability and bioabsorption capacity of the filler, and the film-hanging period can be reduced to 7-14 days.
  • the filler in the biological aerated filter includes at least one of coconut shell charcoal, almond shell charcoal and coal-based activated carbon
  • the filler in a conventional biological filter includes ceramsite, volcanic rock and at least one of zeolites.
  • the specific surface area of the filler in the biological aerated filter in the embodiment of the present disclosure is larger than that of the filler in a conventional biological filter.
  • the biochemical bacteria inoculated in the biological aerated filter usually come from the sewage treatment plant in the market, which is not suitable for the high salt content of the oilfield produced water, which will lead to changes in the osmotic pressure of the added microorganisms, causing the microorganisms to lose water death, and the microbial culture cycle is long, about 90 days, so that the time cost and economic cost are very high.
  • the treatment method of oilfield produced water also includes: adding a salt-tolerant bacteria agent in the biological aerated filter, for example, the quality of the salt-tolerant bacteria agent per cubic meter of oilfield produced water is 5g ⁇ 50g, and the number of effective bacteria in the salt-tolerant bacteria agent per gram of oilfield produced water is greater than or equal to 200 million.
  • the mass of the salt-resistant bacteria agent per cubic meter of oilfield produced water is 10g, 15g, 20g, 25g, 30g, 35g, 40g, 45g or 50g.
  • the way of adding salt-tolerant bacteria is not only easy to implement, but also can strengthen the removal rate of organic matter in the biochemical system, and improve the operation of the biochemical system in cold seasons, and quickly start the new biochemical system. Build new ecosystems.
  • the treatment method of the oilfield produced water also includes: using an ultrafiltration element to perform ultrafiltration treatment on the effluent of the biological aerated filter.
  • the ultrafiltration treatment of the ultrafiltration element can remove impurities such as suspended solids and colloids, and perform advanced pretreatment for the oilfield produced water to enter the subsequent reverse osmosis membrane.
  • the filtration forms of ultrafiltration include but are not limited to hollow ultrafiltration membranes, plate ultrafiltration membranes and tubular ultrafiltration membranes.
  • the materials of ultrafiltration membranes include but are not limited to inorganic ceramic membranes, inorganic silicon carbide membranes, organic polyvinylidene fluoride Ethylene (PVDF) and polytetrafluoroethylene (PTFE), etc.
  • the average pore size of the ultrafiltration membrane is 20-200nm, for example, the flux of the ultrafiltration membrane is 10-35L/m 2 ⁇ h.
  • the method of ultrafiltration treatment has the advantages of no need for dosing, lower operating pressure and stronger operability, and ultrafiltration treatment can separate macromolecules and viruses.
  • the reverse osmosis element includes a reverse osmosis membrane.
  • the form of the reverse osmosis membrane includes but is not limited to a roll-type membrane reverse osmosis element and a disc-type reverse osmosis element.
  • the desalination rate of the reverse osmosis membrane is not lower than 97%.
  • the filtration temperature The temperature does not exceed 45°C, the operating pressure is 0.1-10Mpa, and the flux of the reverse osmosis membrane is 10-25L/m 2 ⁇ h.
  • the treatment method for oilfield produced water provided by at least one embodiment of the present disclosure further includes: using a resin filter to treat the concentrated water after reverse osmosis treatment, and setting the filtration rate to 5BV/h, wherein, Produced water is output from the resin filter.
  • the resin filter is used for ion exchange treatment of oilfield produced water after reverse osmosis treatment to deeply remove calcium and magnesium plasma.
  • the resin filter uses a ceramic membrane cross-flow filter with an average pore size of 50nm.
  • the pressure is controlled at 0.3MPa
  • the flow rate of the membrane surface is controlled at 3m/s
  • the pH of the water produced by the hard filter is adjusted to 6-9
  • the SDI of the water produced by the hard filter is ⁇ 5
  • the recovery rate is not less than 95% .
  • pretreating the oilfield produced water includes: using At least one of the adjustment tank, the nitrogen air flotation unit, the hard and silicon removal unit, the sedimentation tank and the filter unit treats the oilfield produced water.
  • FIG. 3 is a flowchart of a pretreatment section provided by an embodiment of the present disclosure. As shown in FIG. 3, the pretreatment includes:
  • the regulating tank can adjust the acidity and alkalinity of the oilfield produced water, such as adding sodium hydroxide, sodium carbonate, etc. in the sedimentation tank to increase the pH of the originally acidic oilfield produced water to near neutrality, Part of calcium ions, magnesium ions, etc. can be precipitated to be removed.
  • the conventional sedimentation degreasing method has low degreasing efficiency and occupies a large area.
  • the air flotation method can improve the oil removal efficiency and remove suspended matter at the same time, but the air flotation method introduces dissolved oxygen, which can increase the corrosion rate of the water treatment system, because the oilfield produced water usually contains hydrogen sulfide and petroleum hydrocarbons ,
  • the air flotation method accelerates the volatilization of these organic compounds, resulting in peculiar smell in the operating environment, thereby deteriorating the operating environment.
  • a nitrogen air flotation unit can be used for pretreatment, and the nitrogen source in the nitrogen air flotation unit includes nitrogen produced by pressure swing adsorption nitrogen from an air source or a pure nitrogen gas source.
  • nitrogen air flotation can avoid the problem of increasing the corrosion rate caused by the introduction of dissolved oxygen by conventional dissolved air flotation.
  • the top of the nitrogen flotation equipment adopts a sealed design and an inspection port is reserved, and it is equipped with a gas collection and connection pipeline system to collect the odor gas generated by the nitrogen flotation into the gas treatment system for treatment.
  • nitrogen flotation not only avoids the incorporation of external oxygen into oilfield produced water, but also avoids the problem of aggravating the electrochemical corrosion of oilfield produced water, and can also dissolve dissolved gases in oilfield produced water, for example, Aggressive carbon dioxide, dissolved oxygen, hydrogen sulfide, etc. are blown off, which can significantly improve the corrosion characteristics of oilfield produced water and the operating environment of downstream sections.
  • the carrying device of nitrogen air flotation is nitrogen air flotation oil removal device.
  • the nitrogen air flotation oil removal device generates a large number of fine nitrogen bubbles as the carrier through the nitrogen generating device in the oil field produced water to be treated.
  • oil field produced water When oil droplets, impurity flocs and air bubbles adhere to each other, a granule with an overall density lower than that of water is formed.
  • the buoyancy of the granule is greater than gravity and resistance to make it float to the water surface, thus completing the solid-solid, solid-liquid,
  • the slick oil and impurity flocs separated out are discharged out of the system through the bottom sludge discharge system and top slag scraping system to further purify the oilfield produced water, and it is adopted in this application
  • the nitrogen generator produces microporous nitrogen bubbles, thus avoiding the problems of oxygen corrosion and scaling caused by conventional dissolved air flotation technology.
  • the hard and silicon removing unit can adopt lime softening method, lime-soda ash softening method, lime-gypsum treatment method and caustic soda method to perform hard removal treatment.
  • lime softening method is usually used; for water with high hardness and low alkalinity, lime-soda softening method is usually used; for negative hard water with low hardness and high alkalinity, lime-gypsum method is generally used deal with.
  • silicic acid is one of the major impurities in oilfield produced water, mainly derived from the hydrolysis of silicate minerals. Silicon in water generally exists in molecular state, ion state, colloidal state or solid state, and the existence form of silicic acid in water is related to the pH value of water, including dissolved metasilicate, orthosilicic acid, and polymerized state polysilicic acid.
  • the silicon dioxide dissolved in water is mainly in the form of simple silicic acid in the molecular state, and the silicon compound existing in the ion or molecular state is called active silicon, and the size of active silicon is much smaller than that of colloidal silicon, for example , silicon removal treatment can be carried out by adding magnesium agent to water while adding coagulant.
  • the sedimentation tank is a radial flow sedimentation tank, and the effluent quality of the sedimentation tank is: COD 100-350mg/l, petroleum 0.2-3mg/l, and suspended solids 10-30mg/l.
  • the sedimentation tank is any one of a high-efficiency sedimentation tank, a sand-adding sedimentation tank, and a circulating clarification tank.
  • the sedimentation tank Before using the sedimentation tank for treatment, it also includes the treatment with a flocculation tank, the water inlet of the flocculation tank is connected with the water outlet of the hard and silicon removal unit, and the water outlet of the flocculation tank is connected with the water inlet of the sedimentation tank.
  • using a filtration unit for pretreatment may also include using a microfiltration unit for microfiltration treatment.
  • the microfiltration treatment may include cross-flow filtration and dead-end filtration.
  • the average pore size of the filter membrane used in the microfiltration treatment is in the range of 20-200nm, and the operating pressure may be 0.01-1Mpa.
  • the form of the microfiltration membrane includes but is not limited to roll membrane and disk reverse osmosis membrane element, the salt rejection rate of the microfiltration membrane is not lower than 97%, and the filtration temperature of the microfiltration membrane is not higher than 45°C.
  • microfiltration treatment can remove suspended solids and bacteria in oilfield produced water.
  • using a filter unit for pretreatment may also include using a nanofiltration unit for nanofiltration treatment.
  • the nanofiltration unit includes a primary nanofiltration unit and a secondary nanofiltration unit.
  • the primary nanofiltration membrane is used
  • the secondary nanofiltration membrane is used to treat the oilfield produced water.
  • the nanofiltration concentrate can be returned to the ultrafiltration water inlet pipeline.
  • the nanofiltration treatment may include cross-flow filtration and dead-end filtration.
  • the nanofiltration membrane used in the nanofiltration treatment has an average pore size in the range of 10-20 nm and an operating pressure of 0.01-1 Mpa.
  • the membrane elements used in the nanofiltration membrane include but are not limited to tube type, plate type, hollow fiber, roll type nanofiltration membrane and disc type nanofiltration membrane, the rejection rate is not lower than 95%, and the temperature of the nanofiltration membrane is not Above 45°C, the recovery rate of product water is 60%-90%, the membrane flux is 10-40LMH, and the material of the nanofiltration membrane is polyamide.
  • the concentrated water produced by nanofiltration is returned to the biological aerated filter for treatment.
  • nanofiltration treatment can reduce the hardness of oilfield produced water and remove some heavy metals and organic matter.
  • the cleaning method of the nanofiltration membrane is carried out according to the following steps: the first step is to wash the nanofiltration membrane with desalinated water, and discharge the residue in the nanofiltration membrane.
  • the nanofiltration membrane processor After washing the raw water, rinse the nanofiltration membrane for 30 minutes to 60 minutes at normal pressure and 20°C to 25°C; in the second step, use 0.1% ethylenediaminetetraacetic acid, 0.2% sodium pyrophosphate and 0.5% dodecane Wash the nanofiltration membrane processor with a mixture of sodium sulfate for 20 minutes to 40 minutes; the third step is to wash the nanofiltration membrane with hydrochloric acid with a pH value of 2 for 20 minutes to 40 minutes; the fourth step is to rinse the nanofiltration membrane with desalinated water to the pH value of the effluent It is neutral, at this time, the nanofiltration membrane is regenerated.
  • the hardness of oilfield produced water after pretreatment is less than or equal to 200mg/L
  • the density of silicon is less than or equal to 20mg/L
  • the density of petroleum hydrocarbons is less than or equal to 2mg/L
  • the alkalinity is less than or equal to 2000mg/L.
  • FIG. 4 is a flow chart of a method for treating oilfield produced water provided by an embodiment of the present disclosure. The method includes the following steps:
  • the oilfield produced water enters the heat exchange component and the cooling tower in sequence after being pretreated.
  • This step can cool down the pretreated oilfield produced water.
  • the oxidation pond can oxidize and decompose the emulsified and dissolved organic matter in the oilfield produced water, reduce the fouling of the macromolecular organic matter in the oilfield produced water to the subsequent membrane elements, and improve the biodegradability of the oilfield produced water.
  • the organic matter in the produced water of the oil field is further decomposed and mineralized in the biological aerated filter to further reduce membrane fouling, and the backwash water of the biological filter enters the regulating tank in the pretreatment section.
  • the effluent from the biological aerated filter enters the ultrafiltration element and the reverse osmosis element.
  • the ultrafiltration treatment is carried out through the ultrafiltration element to remove impurities such as suspended solids and colloids, and the oilfield produced water enters the reverse osmosis element for advanced treatment. Oilfield formations.
  • the resin filter uses cationic resin, and the backwash water of the resin filter is discharged to the regulating tank.
  • the effluent from the resin filter is used as a cold source in the heat exchange component to exchange heat with the pretreated oilfield produced water, and then enters the steam injection boiler for reuse.
  • FIG. 5 is a schematic diagram of the connection structure of a treatment device for oilfield produced water provided by an embodiment of the present disclosure.
  • the treatment device for produced water includes: oilfield produced water supply part 1 configured to provide oilfield produced water; heat exchange part 2 configured to cool down oilfield produced water; purification part 3 configured to cool oilfield produced water The outlet water is purified to obtain produced water; the water delivery pipe 4 is configured to deliver the produced water, the first end of the heat exchange component 2 is connected to the oilfield produced water supply unit 1, and the second end of the heat exchange component 2 is connected to the water delivery pipe 4 , so that the oilfield produced water and produced water are heat-exchanged in the heat exchange component 2, so as to lower the temperature of the oilfield produced water.
  • the first end of the heat exchange component 2 is connected to the oilfield produced water supply component 1, either directly or through other components.
  • the first end of the heat exchange component 2 There may also be a pretreatment component between the end and the oilfield produced water supply component 1.
  • the water pipe 4 transmits the produced water output from the heat exchange component to other components, such as a cooling tower or a purification component.
  • Figure 6 is a schematic diagram of the connection structure of another oilfield produced water treatment device provided by an embodiment of the present disclosure.
  • the heat exchange component 2 includes a heat exchanger, and the heat exchanger includes a spiral plate heat exchanger Heater or plate heat exchanger.
  • the device for treating oilfield produced water provided by at least one embodiment of the present disclosure further includes a radiator 5 , wherein the radiator 5 is configured to dissipate heat from the oilfield produced water.
  • the radiator 5 is configured to dissipate heat from the oilfield produced water.
  • the oilfield produced water treatment device further includes a cooling tower 6 arranged between the heat exchange component 2 and the purification component 3 .
  • the purification unit 3 includes at least one of an oxidation tank 7 , a biological aerated filter tank 8 , an ultrafiltration element 9 , a reverse osmosis element 10 and a resin filter 11 .
  • the heat exchange unit 2 is directly connected to the oxidation tank 7, the water outlet of the pretreatment section is connected to the hot water inlet of the heat exchange unit 2, and the water outlet pipe of the resin filter 11 is connected to the cold water inlet of the heat exchange unit 2.
  • the resin filter 11 uses a cationic resin material.
  • the water outlet pipe of the resin filter 11 is connected with the cold water end inlet of the heat exchange component 2, so as to realize the heat exchange between the subsequent oilfield produced water and the produced water obtained by cooling and purifying the oilfield produced water, so that the subsequent The temperature of the oilfield produced water decreases and the temperature of the produced water increases.
  • the oxidation cell 7 includes an electrocatalytic oxidation component, or a combination of ozone and hydrogen peroxide, or an electrocatalytic oxidation component, and a combination of ozone and hydrogen peroxide. That is, the oxidation using an oxidation pool includes oxidation with ozone and hydrogen peroxide, or oxidation by electrocatalysis, or a combination of oxidation by ozone and hydrogen peroxide and oxidation by electrocatalysis. Fenton oxidation may be included, which is not limited by embodiments of the present disclosure.
  • the oxidation pond can be used to decompose the emulsified and dissolved organic matter in the oilfield produced water, so as to reduce the fouling of the macromolecular organic matter in the oilfield produced water to the subsequent membrane system, and at the same time improve the biodegradability of the oilfield produced water.
  • the filler in the biological aerated filter 8 is at least one of coconut shell charcoal, apricot shell charcoal, and coal-based activated carbon, and the filler of a conventional biological filter At least one of ceramsite, volcanic rock and zeolite is included.
  • the specific surface area of the filler in the biological aerated filter 8 is larger than the specific surface area of the filler in the conventional biological filter, and the activation process is added on the basis of the filler with a larger specific surface, which can improve the film formation of the filler capacity and biosorption capacity, for example, the film-hanging cycle can be 7-14 days.
  • the treatment device provided in at least one embodiment of the present disclosure also includes a pretreatment unit, wherein the pretreatment unit includes a regulating tank 12, a nitrogen air flotation unit 13, a hard and silicon removal unit 13, a sedimentation tank 15 and a filtration unit 16 at least one of the .
  • the pretreatment unit includes a regulating tank 12, a nitrogen air flotation unit 13, a hard and silicon removal unit 13, a sedimentation tank 15 and a filtration unit 16 at least one of the .
  • the filter unit 16 is directly connected to the heat exchange component 2 .
  • the filtration unit 16 includes a microfiltration unit and a nanofiltration unit
  • the microfiltration unit may be a tubular microfiltration membrane filter
  • the nanofiltration unit may be a membrane-coated fiber ball filter.
  • the regulating tank 12 can adjust the acidity and alkalinity of the oilfield produced water, for example, by applying sodium hydroxide, sodium carbonate, etc. in the sedimentation tank to increase the pH of the originally acidic oilfield produced water to near neutrality, It is also possible to make some calcium ions, magnesium ions, etc. form precipitates to be removed. Alternatively, it is also possible to apply sulfuric acid, hydrochloric acid, nitric acid, etc. in the sedimentation tank to reduce the pH of the originally alkaline oilfield produced water to near neutrality, and also allow some calcium ions, magnesium ions, silver ions, etc. remove.
  • the backwash water of the biological aerated filter 8 enters the regulating tank 12 .
  • the carrying device of nitrogen air flotation is nitrogen air flotation oil removal device.
  • the nitrogen air flotation oil removal device generates a large number of fine nitrogen bubbles as the carrier through the nitrogen generating device in the oil field produced water to be treated.
  • oil field produced water When oil droplets, impurity flocs and air bubbles adhere to each other, a granule with an overall density lower than that of water is formed.
  • the buoyancy of the granule is greater than gravity and resistance to make it float to the water surface, thus completing the solid-solid, solid-liquid,
  • the slick oil and impurity flocs separated out are discharged out of the system through the bottom sludge discharge system and top slag scraping system to further purify the oilfield produced water, and it is adopted in this application
  • the nitrogen generator produces microporous nitrogen bubbles, thus avoiding the problems of oxygen corrosion and scaling caused by conventional dissolved air flotation technology.
  • FIG. 7 is a schematic structural diagram of forming a nitrogen air flotation provided by an embodiment of the present disclosure. As shown in FIG. Nitrogen air flotation, and then the used nitrogen air flotation is transported to the degassing treatment system through a negative pressure fan.
  • nitrogen air flotation can avoid the problem of increasing the corrosion rate caused by the introduction of dissolved oxygen by conventional dissolved air flotation.
  • the top of the nitrogen flotation equipment adopts a sealed design and an inspection port is reserved, and it is equipped with a gas collection and connection pipeline system to collect the odor gas generated by the nitrogen flotation into the gas treatment system for treatment.
  • nitrogen flotation not only avoids the incorporation of external oxygen into oilfield produced water, but also avoids the problem of aggravating the electrochemical corrosion of oilfield produced water, and can also dissolve dissolved gases in oilfield produced water, for example, Aggressive carbon dioxide, dissolved oxygen, hydrogen sulfide, etc. are blown off, which can significantly improve the corrosion characteristics of oilfield produced water and the operating environment of downstream sections.
  • heat exchange is performed between subsequent oilfield produced water and produced water, so that the temperature of subsequent oilfield produced water is lowered, and the temperature of produced water is raised. High, so that the high-temperature oilfield produced water and the clean water after treatment can be exchanged for heat, which not only realizes cooling without an external cold source, but also realizes the reuse of waste heat.
  • the oxidation pond is used to decompose the emulsified and dissolved organic matter in the oilfield produced water, so as to reduce the pollution of macromolecular organic matters in the oilfield produced water to the subsequent membrane system. Plugging, while improving the biodegradability of oilfield produced water.
  • the biological aerated filter replaces the traditional biochemical tank, integrates biological oxidation, biological flocculation and filtration, and does not need to set up a secondary sedimentation tank, which satisfies both The biochemical requirements are met, and the purpose of reducing the floor area and infrastructure investment is achieved.
  • the oxygen transmission efficiency in the biological aerated filter is high, the aeration volume is small, the power consumption of oxygen supply is low, the power consumption of the unit oilfield produced water is low, the degree of automation is high, the operation and management are convenient, and the membrane hanging cycle can be shortened to 14 ⁇ 21 days.

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Abstract

本公开的实施例提供一种油田采出水的处理方法和油田采出水的处理装置，该油田采出水的处理方法包括：提供油田采出水；对所述油田采出水进行降温和净化处理以得到产水；将后续的油田采出水和所述产水进行热交换，以使所述后续的油田采出水的温度降低，且使所述产水的温度升高，从而可以将高温的油田采出水和处理后的清洁产水进行热交换，既实现了不需要外加冷源降温又实现了余热再利用。

Description

油田采出水的处理方法和处理装置
本申请要求于2021年5月17日递交的中国专利申请第202110536509.8号的优先权，在此全文引用上述中国专利申请公开的内容以作为本申请的一部分。
技术领域
本公开的实施例涉及一种油田采出水的处理方法和油田采出水的处理装置。
背景技术
稠油的开采是一个复杂的过程，稠油开采的难度大且成本高。稠油热采是目前最有效、应用范围最广的提高稠油采收率的方法，稠油热采主要包括蒸汽吞吐、蒸汽驱动、蒸汽辅助重力泄油等方式。在稠油热采的过程中需要向地层持续加入高温高压蒸汽以降低原油的粘度，且该过程需要消耗大量的淡水和热能。
稠油采出水具有矿化度高、温度高、硬度大、易形成水包油型乳化液、油水密度差小、硅含量高、污染物含量高等特点。稠油热采的过程中有大量富余的污水被无效回灌，稠油油藏所在地区的生态脆弱，如果将稠油采出水直接排放到外界环境中，不仅会破坏生态环境，还会造成水资源的浪费，给油田水平衡造成了极大的负面影响。油田生产形势日益严峻，且清水资源日益短缺，将富余的稠油采出水处理至可回用的标准，对油田生态环保具有重要的意义，且也可以节约水资源。
发明内容
本公开至少一实施例提供一种油田采出水的处理方法，该方法包括：提供油田采出水；对所述油田采出水进行降温和净化处理以得到产水；将后续的油田采出水和所述产水进行热交换，以使所述后续的油田采出水的温度降低，且使所述产水的温度升高。
例如，在本公开至少一实施例提供的方法中，将所述油田采出水和所述产水进行热交换包括：采用换热部件进行所述热交换，以使所述油田采 出水的温度降低，且使所述产水的温度升高。
例如，本公开至少一实施例提供的方法，在采用换热部件进行所述热交换之后，还包括：采用散热器进行散热。
例如，在本公开至少一实施例提供的方法中，在进行所述热交换之后，还包括：采用冷却塔对所述油田采出水进行再次降温，以使所述油田采出水的温度低于35℃。
例如，在本公开至少一实施例提供的方法中，对所述油田采出水进行净化处理包括：将经过所述降温处理的所述油田采出水采用氧化池进行氧化以分解所述油田采出水中的至少部分有机物。
例如，在本公开至少一实施例提供的方法中，对所述油田采出水进行净化处理包括：采用曝气生物滤池对所述油田采出水进行分解和/或矿化处理以去除所述有机物。
例如，在本公开至少一实施例提供的方法中，在采用曝气生物滤池对所述油田采出水进行分解和/或矿化处理之前，还包括：对所述曝气生物滤池中的填料进行激活处理，其中，对所述曝气生物滤池中的填料进行激活处理包括：采用清水对所述曝气生物滤池进行冲洗，去除所述填料吸附的杂质和/或所述填料被磨损产生的粉末；采用氢氧化钠溶液处理所述填料，去除所述填料包括的有机物杂质，并采用清水对所述填料进行处理至中性；采用硫酸溶液处理所述填料，去除所述填料吸附的无机物，并采用清水对所述填料进行处理至中性。
例如，在本公开至少一实施例提供的方法中，所述曝气生物滤池中的填料包括椰壳炭、杏壳炭和煤质活性炭中的至少之一。
例如，本公开至少一实施例提供的方法，还包括：在所述曝气生物滤池中加入耐盐菌剂，其中，每立方米所述油田采出水中所述耐盐菌剂的质量为5～50g，且每克所述油田采出水中的所述耐盐菌剂中有效菌数大于或者等于2.0亿。
例如，本公开至少一实施例提供的方法，还包括：采用超滤元件对所述曝气生物滤池出水进行超滤处理。
例如，本公开至少一实施例提供的方法，还包括：采用反渗透元件对所述超滤元件出水进行反渗透处理以进行脱盐。
例如，本公开至少一实施例提供的方法，还包括：采用树脂过滤器对经过所述反渗透处理后的浓水进行处理，其中，从所述树脂过滤器输出所述产水。
例如，在本公开至少一实施例提供的方法中，在对所述油田采出水进行降温和净化处理之前，还包括：对所述油田采出水进行预处理，所述预处理包括：采用调节池、氮气气浮单元、除硬除硅单元、沉淀池和过滤单元中的至少之一对所述油田采出水进行处理。
本公开至少一实施例还提供一种油田采出水的处理装置，包括：油田采出水提供部件，配置为提供油田采出水；换热部件，配置为对所述油田采出水进行降温处理；净化部件，配置为对进行降温处理后的所述油田采出水进行净化处理以得到产水；输水管，配置为输送所述产水，其中，所述换热部件的第一端与油田采出水提供部件相连，所述换热部件的第二端与所述输水管相连，使得所述油田采出水和所述产水在所述换热部件中进行热交换，以对所述油田采出水进行降温处理。
例如，在本公开至少一实施例提供的处理装置中，所述换热部件包括换热器。
例如，本公开至少一实施例提供的处理装置，还包括散热器，其中，所述散热器配置为对所述油田采出水进行散热。
例如，本公开至少一实施例提供的处理装置，还包括冷却塔，其中，所述冷却塔设置在所述换热部件和所述净化部件之间。
例如，在本公开至少一实施例提供的处理装置中，所述净化部件包括氧化池、曝气生物滤池、超滤元件、反渗透元件和树脂过滤器中的至少之一。
例如，在本公开至少一实施例提供的处理装置中，所述氧化池包括电催化氧化部件，或者臭氧与双氧水的组合，或者电催化氧化部件，和臭氧与双氧水的组合。
例如，在本公开至少一实施例提供的处理装置中，所述曝气生物滤池中的填料为椰壳炭、杏壳炭和煤质活性炭中的至少之一。
例如，本公开至少一实施例提供的处理装置，还包括预处理部件，其中，所述预处理部件包括调节池、氮气气浮单元、除硬除硅单元、沉淀池 和过滤单元中的至少之一。
例如，在本公开至少一实施例提供的处理装置中，所述过滤单元包括覆膜纤维球过滤器和管式微滤膜过滤器。
附图说明
为了更清楚地说明本公开实施例的技术方案，下面将对实施例的附图作简单地介绍，显而易见地，下面描述中的附图仅仅涉及本公开的一些实施例，而非对本公开的限制。
图1为本公开一实施例提供的一种油田采出水的处理方法的流程图；
图2为本公开一实施例提供的一种油田采出水的处理方法的过程图；
图3为本公开一实施例提供的预处理工段的流程图；
图4为本公开一实施例提供的一种油田采出水的处理方法的流程图；
图5为本公开一实施例提供的一种油田采出水的处理装置的连接结构示意图；
图6为本公开一实施例提供的再一种油田采出水的处理装置的连接结构示意图；以及
图7为本公开一实施例提供的一种形成氮气气浮的结构示意图。
具体实施方式
为使本公开实施例的目的、技术方案和优点更加清楚，下面将结合本公开实施例的附图，对本公开实施例的技术方案进行清楚、完整地描述。显然，所描述的实施例是本公开的一部分实施例，而不是全部的实施例。基于所描述的本公开的实施例，本领域普通技术人员在无需创造性劳动的前提下所获得的所有其他实施例，都属于本公开保护的范围。
除非另外定义，本公开使用的技术术语或者科学术语应当为本公开所属领域内具有一般技能的人士所理解的通常意义。本公开中使用的“第一”、“第二”以及类似的词语并不表示任何顺序、数量或者重要性，而只是用来区分不同的组成部分。“包括”或者“包含”等类似的词语意指出现该词前面的元件或者物件涵盖出现在该词后面列举的元件或者物件及其等同，而不排除其他元件或者物件。“连接”或者“相连”等类似的词语并非限定于物理的或者机械的连接，而是可以包括电性的连接，不管是直接的还是间接的。 “上”、“下”、“顶”、“底”等仅用于表示相对位置关系，当被描述对象的绝对位置改变后，则该相对位置关系也可能相应地改变。
注汽锅炉水对含盐量要求较高，油田采出水回用做注汽锅炉水的处理技术主要包括热法处理和膜法处理两种方式。热法处理技术即采用蒸发脱盐的方式回收蒸馏水，采用的设备包括机械式蒸汽再压缩(MVR)、机械蒸汽压缩器(MVC)或者多效蒸发器等。采用该方式能够回收80％以上高质量的蒸馏水。此外，蒸馏水的回收率与油田采出水中盐分的含量有关，处理的油田采出水中盐的浓度越高，蒸发所需要的能量越高，水的气化潜热越高，水从液态变成气态发生相变所需要的能量越高。即热法处理技术需要消耗大量蒸汽加热或电能升温，处理成本较高，且所使用的设备的体积庞大。此外，通常油田采出水中氯含量高、盐含量高，处理油田采出水时对高温运行的蒸发装置的材质要求极高，从而导致了热法处理技术在设备投资和运行成本上均较高。膜法处理技术在处理成本和设备投资方面均显著低于热法处理技术，膜法处理技术采用的的主要设备包括超滤膜(UF)、纳滤膜(NF)和反渗透膜(RO)等，一般这些膜组件承受的极限温度为45℃，因此，在较高的温度下处理油田采出水时，会对这些膜组件产生损伤。油田采出水，例如，稠油采出水的温度基本在70℃左右，因此，需要将油田采出水的温度先下降到35～45℃以下，然后对降温后的油田采出水进行处理时，这些膜组件才能正常运行。
本公开的发明人注意到，目前的膜法处理方式只有散热降温的过程，热能无法回收利用，可以在将油田采出水的温度从70℃左右降至35～45℃的过程中，对这一部分热能进行回收利用，即将后续待处理的高温的油田采出水和处理过的油田采出水得到的清洁产水进行热交换，既实现了不需外加冷源对后续待处理的高温的油田采出水进行降温又实现了余热回用，从而实现了节能减排。
本公开至少一实施例提供一种油田采出水的处理方法，该方法包括：提供油田采出水；对油田采出水进行降温和净化处理以得到产水；将后续的油田采出水和产水进行热交换，以使后续的油田采出水的温度降低，且使产水的温度升高。
例如，图1为本公开一实施例提供的一种油田采出水的处理方法的流程图，包括如下步骤：
步骤S01:提供油田采出水。
例如，该油田采出水为稠油采出水。在开采稠油的过程中需要采用热采锅炉注蒸汽进行采取，即向地层持续加入高温高压蒸汽以降低原油的粘度，因此，未经处理之前稠油采出水的温度通常在70℃左右，此外，稠油采出水具有采出液粘度高、携沙量大、硬度高和矿化度高的特点。
步骤S02:对油田采出水进行降温和净化处理以得到产水。
在该步骤中，需要外加冷源对初始的油田采出水进行降温处理。
步骤S03:将后续的油田采出水和产水进行热交换，以使后续的油田采出水的温度降低，且使产水的温度升高。
例如，注汽锅炉水对含盐量要求较高，只能是清水，且需要具有一定的温度，因此，该温度升高后的产水可以回用作注气锅炉水。
例如，将油田采出水和产水进行热交换包括：采用换热部件进行热交换，以使油田采出水的温度降低，且使产水的温度升高。例如，该换热部件的第一端与油田采出水输入的管件相连，换热部件的第二端与传输产水的输水管相连，油田采出水和产水逆向流动，使得油田采出水和产水在换热部件中进行热交换，以对油田采出水进行降温处理，且使得产水的温度升高，以备用作注气锅炉水。
例如，换热部件包括螺旋板式换热器或者板式换热器，该换热部件包括高效板式换热设备，该高效板式换热设备是可拆卸的，这样可以实现安装、运输等的便利性。该高效板式换热设备例如由钛合金材料形成，例如，钛钢合金，从而高效板式换热设备可以承受500-550℃的温度。
例如，图2为本公开一实施例提供的一种油田采出水的处理方法的过程图，如图2所示，在采用换热部件进行热交换之后，还包括：采用散热器进行散热。
例如，采用散热器可以对油田采出水进行进一步地降温，以减少后续对超滤膜(UF)、纳滤膜(NF)和反渗透膜(RO)造成损坏的风险，此外，将换热部件和散热器联用，可以降低散热器的负荷以及设备投资，即相比于不采用换热部件换热，而直接采用散热器散热的情形，可以使得散热器的负荷减小，使得散热器的寿命不缩短。
例如，如图2所示，在进行热交换之后，该处理方法还可以包括：采用冷却塔对油田采出水进行再次降温，以使得油田采出水的温度低于35℃，这 样将温度低于35℃的油田采出水输入至后续的超滤膜(UF)、纳滤膜(NF)和反渗透膜(RO)进行处理时，不会由于温度太高对这些膜部件造成影响。
例如，在一个示例中，该冷却塔为闭式冷却塔，冷却塔用水作为循环冷却剂，循环冷却剂和油田采出水位于不同的管道中，循环冷却剂从油田采出水中吸收热量以降低油田采出水的温度，然后循环冷却剂将热量排放至大气中，以降低循环冷却水的温度。
例如，在另一个示例中，冷却塔和散热器直接连接，以对油田采出水进行进一步降温，且冷却塔使用的是冷风冷却的方式。
例如，如图2所示，对油田采出水进行净化处理包括：将经过降温处理的油田采出水采用氧化池进行氧化以分解油田采出水中的至少部分有机物。
例如，采用氧化池进行氧化包括采用臭氧和双氧水进行氧化，或者采用电催化的方式进行氧化，或者还可以是采用臭氧和双氧水进行氧化与采用电催化的方式进行氧化的方式的组合，该氧化还可以包括芬顿氧化，本公开的实施例对此不作限定。
例如，分解油田采出水中的至少部分有机物包括利用氧化池分解油田采出水中乳化、溶解的有机物，减轻油田采出水中大分子的有机物对后续采用的膜系统的污堵，同时提高油田采出水的可生化性。
例如，常规的隔油、气浮、吸附、过滤等预处理方式不能大幅去除溶解和乳化的有机物，油田采出水中的化学需氧量(COD)仍然偏高，约为400～600mg/L。高化学需氧量(COD)易造成膜处理系统的污堵，且有机污染物不容易反洗，膜通量下降后也不容易恢复。
例如，氧化池中臭氧的浓度为5-30mg/L，氧化池氧化的时间小于或者等于10min。经该步骤处理之后，形成的产水COD(化学需氧量)小于45mg/L。例如，臭氧热氧化可以大大提高臭氧对油田采出水中难降解有机物的处理效果。
本公开的实施例在常规的预处理的基础上增加了氧化池，该氧化池可以分解油田采出水中溶解和乳化的有机物，从而可以减轻对膜设备的污堵。氧化池处理后的油田采出水进入生化处理单元，以深度矿化有机物，从而可以进一步减轻有机物对膜通量的影响。
例如，采用氧化池的处理方式可以直接用于油田采出水的处理，不仅可以确保油田采出水的处理效果，还可以大大降低处理成本，整个工艺流程简 单，可操作性强。
例如，油田采出水采用氧化池处理后进入生化处理单元，该生化处理单元可以深度矿化有机物，以进一步减轻有机物对膜通量的影响。
例如，如图2所示，对油田采出水进行净化处理包括：采用曝气生物滤池(BAF)对油田采出水进行分解和矿化处理中的至少之一以去除有机物。
例如，在曝气生物滤池中装有塑料蜂窝填料，填料被水浸没，用鼓风机在填料底部曝气充氧进行鼓风曝气。空气能自下而上夹带待处理的油田采出水，自由通过滤料部分到达地面，空气逸出后曝气生物滤池则在滤料间隔处自上向下返回曝气生物滤池的池底。活性岩屑附着在填料表面，不随水流动，生物膜直接受到上升气流的强烈搅动不断更新，净化效果得到了很大的提高。好氧处理工艺采用接触氧化生物膜法技术，可显著去除油田采出水中溶解性有机污染物和胶体有机污染物。
例如，曝气生物滤池是以装载的粒状填料为载体，以颗粒状填料及其附着生长的生物膜为主要处理介质，充分发挥生物代谢作用，生物絮凝作用，物理过滤作用，以及膜及填料的物理吸附和截留作用，以实现对有机污染物的高效去除。
例如，曝气生物滤池(BAF)可以起到过滤悬浮物，以及降低可生物降解物质的浓度的目的。
例如，曝气生物滤池由池体、滤料、承托层、布水布气系统、反冲洗系统、出水系统和自控系统等组成；曝气生物滤池的池体可以为常规的反应器，反应器内可以使用填料，曝气生物滤池的规模可以根据循环水量以及循环水中污染物的浓度来确定。例如，还可以根据需要设置相应的控制系统、动力系统和监测系统等。
例如，采用曝气生物滤池对油田采出水进行分解和矿化处理是深度去除有机物污染物所采用的主要方式之一，传统的生化池占地面积大，挂膜周期长达30～40天，曝气量大，使用成本较高。使用曝气生物滤池代替传统的生化池，集生物氧化、生物絮凝和过滤于一体，不需要设置二沉池，既满足了生化要求，又达到了减少占地面积和基建投资的目的。曝气生物滤池中氧的传输效率高，曝气量小，供氧动力消耗低，处理单位油田采出水的电耗低，自动化程度高，运行管理方便，且挂膜周期可以缩短到14～21天。
例如，曝气生物滤池技术的大流量内循环流的水力学特征与其传质速度 快、微生物种类多、活性高的特性，将高浓度油田采出水中的有机物进行快速降解，以达到了初步降解油田采出水中有机物的目的。
例如，曝气生物滤池的运行时间为24h～72h，例如为24h、36h、48h或者72h。曝气生物滤池需要进行反冲洗，反冲洗采用气水联动操作，反冲洗总的时间为1小时，其中包括0.5小时的反冲洗时间和0.5小时的恢复时间。内循环曝气生物滤池反冲洗风采用非净化风，反冲洗的风压大于0.45MPa，反冲洗风量为处理水量的2-3倍。
例如，反冲洗水采用反冲洗沉淀池的上清液，反冲洗水量为处理水量的1.6-2.0倍。例如，反冲洗排水进入反冲洗沉淀池进行泥水分离，经静止沉淀后，上清液用作下一次反冲洗的反冲洗水。
例如，在本公开至少一实施例提供的方法中，在采用曝气生物滤池对油田采出水进行分解和/或矿化处理之前，还包括：对曝气生物滤池中的填料进行激活处理，其中，对曝气生物滤池中的填料进行激活处理包括：采用清水对曝气生物滤池进行冲洗，去除填料吸附的杂质和填料被磨损产生的粉末中的至少之一，采用氢氧化钠溶液处理填料，去除填料包括的有机物杂质，并采用清水对填料进行处理至中性，然后采用硫酸溶液处理该填料，以去除填料吸附的无机物，并采用清水对填料进行处理以至中性。
例如，常规的曝气生物滤池中的填料都是直接使用，在加工、运输和包装填料的过程中会对填料产生灰尘、黏土、油脂等污染。目前的加工工艺导致填料内部的微观空隙一定程度上不够畅通或存在堵塞，从而使得滤料的吸附效果变差，有效比表面缩小，从而影响挂膜周期。
例如，装填填料后的激活工序包括：采用清水对曝气生物滤池进行冲洗，去除填料吸附的杂质和/或填料被磨损产生的粉末；采用氢氧化钠溶液处理填料，去除填料包括的有机物杂质，并采用清水对填料进行处理至中性；采用硫酸溶液处理填料，去除填料吸附的无机物，并采用清水对填料进行处理至中性。
例如，在一个示例中，装填填料后具体的激活工序包括：第一步先用清水冲洗2～3遍，清洗掉滤料吸附的杂物和滤料磨损产生的无效粉末；第二步用5％的氢氧化钠清洗浸泡填料4h，以除去填料表面的油脂及有机物；排空氢氧化钠碱液后，用清水冲洗至中性；第三步，使用5％的硫酸清洗浸泡4h，酸化清洁填料的喉道空隙，溶解填料内外部吸附的杂物。
例如，该激活工序可以提高填料的挂膜能力和生物吸附能力，该挂膜周期可以减少到7～14天。
例如，在本公开的一个实施例中，该曝气生物滤池中的填料包括椰壳炭、杏壳炭和煤质活性炭中的至少之一，常规的生物滤池的填料包括陶粒、火山岩和沸石中的至少之一。本公开实施例中曝气生物滤池中的填料的比表面积比常规的生物滤池的填料的比表面积大。
例如，曝气生物滤池接种的生化菌种，通常来自市场的污水处理厂，不适应油田采出水中高含盐的工况，从而导致加入的微生物体内的渗透压发生改变，使得微生物失水死亡，且微生物培养循化周期长，约90天左右，从而使得时间成本和经济成本都很高。
例如，在本公开的实施例中，油田采出水的处理方法还包括：在曝气生物滤池中加入耐盐菌剂，例如，每立方米油田采出水中耐盐菌剂的质量为5g～50g，且每克油田采出水中的耐盐菌剂中有效菌数大于或者等于2.0亿。
例如，在一些示例中，每立方米油田采出水中耐盐菌剂的质量为10g、15g、20g、25g、30g、35g、40g、45g或者50g。
例如，添加耐盐菌剂的方式不仅容易实现，还可以强化生化系统中有机物的去除率，并改善寒冷季节时生化系统的运行状况，快速启动新建的生化系统，例如，可以在14～21天建立新的生态系统。
例如，如图2所示，该油田采出水的处理方法还包括：采用超滤元件对曝气生物滤池出水进行超滤处理。例如，通过超滤元件的超滤处理可以去除悬浮物、胶体等杂质，为油田采出水进入后续的反渗透膜做深度的预处理。
例如，超滤的过滤形式包括但不限于中空超滤膜、板式超滤膜和管式超滤膜，超滤膜的材质包括但不局限于无机陶瓷膜、无机碳化硅膜、有机聚偏氟乙烯(PVDF)和聚四氟乙烯(PTFE)等，超滤膜的平均孔径为20-200nm，例如，超滤膜的通量为10～35L/m 2·h。采用超滤处理的方式具有无需加药、运行压力更低和可操作性更强的优点，且超滤处理可以分离大分子和病毒。
例如，如图2所示，本公开至少一实施例提供的油田采出水的处理方法，还包括：采用反渗透元件对超滤元件的出水进行反渗透处理以进行脱盐。例如，该反渗透元件包括反渗透膜，该反渗透膜的形式包括但不限于卷式膜反渗透元件和碟片式反渗透元件，该反渗透膜的脱盐率不低于97％，过滤温度不超过45℃，操作压力为0.1-10Mpa，该反渗透膜的通量为10～25L/m 2·h。
例如，如图2所示本公开至少一实施例提供的油田采出水的处理方法还包括：采用树脂过滤器对经过反渗透处理后的浓水进行处理，设定滤速5BV/h，其中，从树脂过滤器输出产水，树脂过滤器用于对反渗透处理后的油田采出水进行离子交换处理以深度去除钙、镁等离子，该树脂过滤器采用平均孔径为50nm的陶瓷膜错流过滤器进行过滤，压力控制在0.3MPa，膜面流速控制在3m/s，除硬过滤器的产水调整pH至6-9之间，除硬过滤器产水SDI≤5，回收率不低于95％。
例如，如图2所示，在本公开至少一实施例提供的方法中，在对油田采出水进行降温和净化处理之前，还包括：对油田采出水进行预处理，该预处理工段包括：采用调节池、氮气气浮单元、除硬除硅单元、沉淀池和过滤单元中的至少之一对油田采出水进行处理。
例如，图3为本公开一实施例提供的预处理工段的流程图，如图3所示，该预处理包括：
S11：将油田采出水输入至调节池。
例如，该调节池可以对油田采出水的酸碱性进行调节，例如通过在沉淀池中施加氢氧化钠、碳酸钠等使得原本偏酸性的油田采出水的pH增大至接近中性，还可以使得部分钙离子，镁离子等形成沉淀以被去除。或者，还可以在沉淀池中施加硫酸、盐酸、硝酸等使得原本偏碱性的油田采出水的pH减小至接近中性，还可以使得部分钙离子、镁离子、银离子等形成沉淀以被去除。
S12：将从沉淀池输出的油田采出水输入氮气气浮单元。
例如，常规的沉降除油方法，除油效率低，占地面积大。使用气浮方法可以提高除油效率，同时还可以去除悬浮物，但气浮方法引入了溶解氧，溶解氧能够增加水处理系统的腐蚀速率，由于油田采出水通常含硫化氢和石油烃类物质，气浮方法加速了这些有机物的挥发，导致操作环境中有异味，从而恶化操作环境。例如，可以采用氮气气浮单元进行预处理，氮气气浮单元中的氮气源包括以空气源变压吸附制氮产生的氮气或者纯氮气气源。
例如，采用氮气气浮，可以避免常规溶气气浮引入溶解氧，增加腐蚀速率的问题。氮气气浮的设备的顶部采用密封设计并预留有检修口，并配套设计有气体收集和接引管路的系统，将氮气气浮产生的异味气体收集到气处理系统中进行处理。相对于空气气浮，氮气气浮不仅避免了外界氧气融入油田 采出水，还避免了其可能导致的加剧油田采出水电化学腐蚀的问题，还能够将油田采出水中的溶解性气体，例如，侵蚀性二氧化碳、溶解氧、硫化氢等进行吹脱，从而能够显著改善油田采出水的腐蚀特性及下游工段的操作环境。
例如，氮气气浮的承载装置为氮气气浮除油装置，氮气气浮除油装置是在待处理的油田采出水中通过氮气发生装置产生大量的微细氮气气泡为载体，当油田采出水中的油滴及杂质絮粒与气泡相互粘附时，便形成整体密度小于水的粒团，该粒团的浮力大于重力和阻力使其上浮至水面，从而完成了水中固体与固体、固体与液体、液体与液体分离的过程，同时通过底部排泥系统和顶部刮渣系统将分理出的浮油和杂质絮体排出系统之外，起到进一步净化油田采出水的作用，且在本申请中采用制氮机制造微孔氮气气泡，从而避免了常规溶气气浮技术带来的氧腐蚀和结垢等问题。
S13：将从氮气气浮单元输出的油田采出水输入除硬除硅单元。
例如，该除硬除硅单元可以采用石灰软化法、石灰-纯碱软化法、石灰-石膏处理法及片碱法等进行除硬处理。对硬度高、碱度高的水，通常采用石灰软化法；对硬度高、碱度低的水通常采用石灰-纯碱软化法；而对硬度低、碱度高的负硬水一般采用石灰-石膏法处理。
例如，硅酸是油田采出水中的主要杂质之一，主要来源于硅酸盐矿物质的水解。水体中的硅一般会以分子状态、离子状态、胶体状态或者固体状态存在，而硅酸在水中的存在形态与水的pH值相关，包括溶解态的偏硅酸、正硅酸，还有聚合态的多硅酸。当pH值不高时，溶于水的二氧化硅主要呈分子态的简单硅酸形态，以离子或者分子状态存在的硅化合物称为活性硅，活性硅的尺寸比胶体硅小得多，例如，可以通过在加入混凝剂的同时向水中加入镁剂以进行除硅处理。
S14：将从除硬除硅单元输出的油田采出水输入沉淀池。
例如，该沉淀池为辐流式沉淀池，沉淀池出水水质为：COD 100～350mg/l、石油类0.2～3mg/l，悬浮物10～30mg/l。
例如，该沉淀池为高效沉淀池、加砂沉淀池、循环澄清池中的任意一种。在采用沉淀池进行处理之前，还包括采用絮凝池进行处理，絮凝池的进水口与除硬除硅单元的出水口相连，絮凝池的出水口与沉淀池的进水口相连。
S15：将从沉淀池输出的油田采出水输入过滤单元。
例如，采用过滤单元进行预处理还可以包括采用微滤单元进行微滤处理。该微滤处理可以包括错流过滤和死端过滤两种方式，微滤处理所采用的过滤膜的平均孔径范围为20-200nm，操作压力可以为0.01-1Mpa。例如，该微滤膜的形式包括但不局限于卷式膜、碟片式反渗透膜元件，微滤膜的脱盐率不低于97％，微滤膜的过滤温度不超过45℃。例如，微滤处理可以去除油田采出水中的悬浮物和细菌。
例如，采用过滤单元进行预处理还可以包括采用纳滤单元进行纳滤处理。纳滤单元包括一级纳滤单元和二级纳滤单元，当油田采出水中钙离子的含量低于1500mg/L、溶解性固体的总量低于25000mg/L时，采用一级纳滤膜处理油田采出水，当油田采出水中钙离子的含量高于1500mg/L、溶解性固体总量高于25000mg/L时，采用二级纳滤膜处理油田采出水。采用一级纳滤膜和/或二级纳滤膜处理油田采出水时，纳滤浓缩液均可以回流至超滤进水管路。例如，该纳滤处理可以包括错流过滤和死端过滤两种方式，纳滤处理所采用的纳滤膜的平均孔径范围为10-20nm，操作压力可以为0.01-1Mpa。例如，该纳滤膜采用的膜元件包含但不局限于管式、板式、中空纤维、卷式纳滤膜和碟片式纳滤膜，截留率不低于95％，纳滤膜的温度不超过45℃，产水的回收率为60％-90％，膜通量为10-40LMH，纳滤膜材质为聚酰胺。纳滤过滤产生的浓水回到曝气生物滤池处理。例如，纳滤处理可以减小油田采出水的硬度，并去除部分重金属和有机物。
例如，纳滤膜处理器中的纳滤膜的通量下降15％时，纳滤膜的清洗方法按照下述步骤进行：第一步，用除盐水冲洗纳滤膜，排出残留在纳滤膜的原水后，在常压、20℃至25℃条件下冲洗纳滤膜30min至60min；第二步，采用0.1％的乙二胺四乙酸、0.2％的焦磷酸钠和0.5％的十二烷基硫酸钠的混合液清洗纳滤膜处理器20min至40min；第三步，用pH值为2的盐酸清洗纳滤膜20min至40min；第四步，用除盐水冲洗纳滤膜至出水pH值呈中性，此时，纳滤膜完成再生。
例如，油田采出水经过预处理后的硬度小于或者等于200mg/L，硅的密度小于或者等于20mg/L，石油烃的密度小于或者等于2mg/L，碱度小于或者等于2000mg/L。
例如，图4为本公开一实施例提供的一种油田采出水的处理方法的流程图，该处理方法包括如下步骤：
S21、油田采出水经过预处理后依次进入换热部件、冷却塔。
该步骤可以对进行过预处理的油田采出水进行降温。
S22、降温后的油田采出水进入氧化池。
例如，利用氧化池可以氧化分解油田采出水中乳化、溶解的有机物，减轻油田采出水中大分子的有机物对后续采用的膜元件的污堵，同时提高油田采出水的可生化性。
S23、经过氧化池氧化后的油田采出水进入曝气生物滤池。
例如，油田采出水中的有机物在曝气生物滤池内进一步被分解和矿化，进一步减轻膜污堵，生物滤池的返洗水进入预处理工段的调节池。
S24、曝气生物滤池出水进入超滤元件和反渗透元件。
例如，通过超滤元件进行超滤处理以去除悬浮物、胶体等杂质，为油田采出水进入反渗透元件做深度处理，该反渗透元件可以实现脱盐功能，反渗透元件产生的浓水回注到油田地层。
S25、经过反渗透元件脱盐后的浓水进入树脂过滤器。
例如，该树脂过滤器采用阳离子树脂，树脂过滤器的反洗水排放到调节池。
S26、树脂过滤器出水作为冷源在换热部件内和预处理后油田采出水进行换热后，进入注汽锅炉回用。
本公开至少一实施例还提供一种油田采出水的处理装置，例如，图5为本公开一实施例提供的一种油田采出水的处理装置的连接结构示意图，如图5所示，该油田采出水的处理装置包括：油田采出水提供部件1，配置为提供油田采出水；换热部件2，配置为对油田采出水进行降温处理；净化部件3，配置为对进行降温处理后的油田采出水进行净化处理以得到产水；输水管4，配置为输送产水，该换热部件2的第一端与油田采出水提供部件1相连，换热部件2的第二端与输水管4相连，使得油田采出水和产水在换热部件2中进行热交换，以对油田采出水进行降温处理。
例如，换热部件2的第一端与油田采出水提供部件1相连，可以是直接相连，也可以是通过其他部件相连，例如，在本公开的一个示例中，在换热部件2的第一端与油田采出水提供部件1之间还可以具有预处理部件。
例如，该输水管4是将从换热部件输出的产水向其他部件，例如，冷却塔或者净化部件进行传输。
例如，图6为本公开一实施例提供的再一种油田采出水的处理装置的连接结构示意图，如图6所示，该换热部件2包括换热器，该换热器包括螺旋板式换热器或者板式换热器。
例如，如图6所示，本公开至少一实施例提供的油田采出水的处理装置，还包括散热器5，其中，散热器5配置为对油田采出水进行散热。采用换热部件2和散热器5联用，可以降低散热器5的负荷以及设备投资。
例如，如图6所示，该油田采出水的处理装置还包括冷却塔6，该冷却塔6设置在换热部件2和净化部件3之间。
例如，如图6所示，该净化部件3包括氧化池7、曝气生物滤池8、超滤元件9、反渗透元件10和树脂过滤器11中的至少之一。
例如，换热部件2和氧化池7直接连接，预处理工段的出水口和换热部件2的热水端进口相连，树脂过滤器11的出水管和换热部件2的冷水端进口相连。
例如，该树脂过滤器11采用阳离子树脂材料。例如，树脂过滤器11的出水管和换热部件2的冷水端进口相连，以实现将后续的油田采出水和对油田采出水进行降温和净化处理得到的产水进行热交换，以使后续的油田采出水的温度降低，且使产水的温度升高。
例如，如图6所示，该氧化池7包括电催化氧化部件，或者臭氧与双氧水的组合，或者电催化氧化部件，和臭氧与双氧水的组合。即采用氧化池进行氧化包括采用臭氧和双氧水进行氧化，或者采用电催化的方式进行氧化，或者还可以是采用臭氧和双氧水进行氧化与采用电催化的方式进行氧化的方式的组合，该氧化方式还可以包括芬顿氧化，本公开的实施例对此不作限定。
例如，可以利用氧化池分解油田采出水中乳化、溶解的有机物，以减轻油田采出水中大分子的有机物对后续采用的膜系统的污堵，同时提高油田采出水的可生化性。
例如，在本公开至少一实施例提供的处理装置中，该曝气生物滤池8中的填料为椰壳炭、杏壳炭和煤质活性炭中的至少之一，常规的生物滤池的填料包括陶粒、火山岩和沸石中的至少之一。本公开实施例中曝气生物滤池8中的填料的比表面积比常规的生物滤池的填料的比表面积大，且在比表面大的填料的基础上增加激活工序，可以提高填料的挂膜能力和生物吸附能力， 例如，挂膜周期可以为7～14天。
例如，本公开至少一实施例提供的处理装置，还包括预处理部件，其中，该预处理部件包括调节池12、氮气气浮单元13、除硬除硅单元13、沉淀池15和过滤单元16中的至少之一。
例如，如图6所示，该过滤单元16和换热部件2直接连接。
例如，在本公开至少一实施例提供的处理装置中，该过滤单元16包括微滤单元和纳滤单元，该微滤单元可以为管式微滤膜过滤器，该纳滤单元可以为覆膜纤维球过滤器。
例如，该调节池12可以对油田采出水的酸碱性进行调节，例如通过在沉淀池中施加氢氧化钠、碳酸钠等使得原本偏酸性的油田采出水的pH增大至接近中性，还可以使得部分钙离子，镁离子等形成沉淀以被去除。或者，还可以在沉淀池中施加硫酸、盐酸、硝酸等使得原本偏碱性的油田采出水的pH减小至接近中性，还可以使得部分钙离子、镁离子、银离子等形成沉淀以被去除。
例如，曝气生物滤池8的返洗水进入调节池12。
例如，氮气气浮的承载装置为氮气气浮除油装置，氮气气浮除油装置是在待处理的油田采出水中通过氮气发生装置产生大量的微细氮气气泡为载体，当油田采出水中的油滴及杂质絮粒与气泡相互粘附时，便形成整体密度小于水的粒团，该粒团的浮力大于重力和阻力使其上浮至水面，从而完成了水中固体与固体、固体与液体、液体与液体分离的过程，同时通过底部排泥系统和顶部刮渣系统将分理出的浮油和杂质絮体排出系统之外，起到进一步净化油田采出水的作用，且在本申请中采用制氮机制造微孔氮气气泡，从而避免了常规溶气气浮技术带来的氧腐蚀和结垢等问题。
例如，图7为本公开一实施例提供的一种形成氮气气浮的结构示意图，如图7所示，氮气源系统(例如，制氮机)将氮气输送至氮气气浮的承载装置以形成氮气气浮，然后将使用完的氮气气浮通过负压风机输送至去气处理系统。
例如，采用氮气气浮，可以避免常规溶气气浮引入溶解氧，增加腐蚀速率的问题。氮气气浮的设备的顶部采用密封设计并预留有检修口，并配套设计有气体收集和接引管路的系统，将氮气气浮产生的异味气体收集到气处理系统中进行处理。相对于空气气浮，氮气气浮不仅避免了外界氧气融入油田 采出水，还避免了其可能导致的加剧油田采出水电化学腐蚀的问题，还能够将油田采出水中的溶解性气体，例如，侵蚀性二氧化碳、溶解氧、硫化氢等进行吹脱，从而能够显著改善油田采出水的腐蚀特性及下游工段的操作环境。
本公开的实施例提供的油田采出水的处理方法和油田采出水的处理装置，具有以下至少一项有益效果：
(1)本公开至少一实施例提供的油田采出水的处理方法中，将后续的油田采出水和产水进行热交换，以使后续的油田采出水的温度降低，且使产水的温度升高，从而可以将高温的油田采出水和处理后的清洁产水进行热交换，既实现了不需要外加冷源降温又实现了余热再利用。
(2)本公开至少一实施例提供的油田采出水的处理方法中，利用氧化池分解油田采出水中乳化、溶解的有机物，减轻油田采出水中大分子的有机物对后续采用的膜系统的污堵，同时提高油田采出水的可生化性。
(3)本公开至少一实施例提供的油田采出水的处理方法中，曝气生物滤池代替传统的生化池，集生物氧化、生物絮凝和过滤于一体，不需要设置二沉池，既满足了生化要求，又达到了减少占地面积和基建投资的目的。曝气生物滤池中氧的传输效率高，曝气量小，供氧动力消耗低，处理单位油田采出水的电耗低，自动化程度高，运行管理方便，且挂膜周期可以缩短到14～21天。
有以下几点需要说明：
(1)本公开实施例附图只涉及到与本公开实施例涉及到的结构，其他结构可参考通常设计。
(2)为了清晰起见，在用于描述本公开的实施例的附图中，层或区域的厚度被放大或缩小，即这些附图并非按照实际的比例绘制。可以理解，当诸如层、膜、区域或基板之类的元件被称作位于另一元件“上”或“下”时，该元件可以“直接”位于另一元件“上”或“下”，或者可以存在中间元件。
(3)在不冲突的情况下，本公开的实施例及实施例中的特征可以相互组合以得到新的实施例。
以上所述，仅为本公开的具体实施方式，但本公开的保护范围并不局限于此，本公开的保护范围应以所述权利要求的保护范围为准。

Claims (22)

  1. 一种油田采出水的处理方法，包括：
    提供油田采出水；
    对所述油田采出水进行降温和净化处理以得到产水；
    将后续的油田采出水和所述产水进行热交换，以使所述后续的油田采出水的温度降低，且使所述产水的温度升高。
  2. 根据权利要求1所述的方法，其中，将所述后续的油田采出水和所述产水进行热交换包括：采用换热部件进行所述热交换，以使所述后续的油田采出水的温度降低，且使所述产水的温度升高。
  3. 根据权利要求2所述的方法，在采用所述换热部件进行所述热交换之后，还包括：采用散热器进行散热。
  4. 根据权利要求1-3中任一项所述的方法，其中，在进行所述热交换之后，还包括：采用冷却塔对所述油田采出水进行再次降温，以使所述油田采出水的温度低于35℃。
  5. 根据权利要求1-4中任一项所述的方法，其中，对所述油田采出水进行净化处理包括：将经过所述降温处理的所述油田采出水采用氧化池进行氧化以分解所述油田采出水中的至少部分有机物。
  6. 根据权利要求1-5中任一项所述的方法，其中，对所述油田采出水进行净化处理包括：采用曝气生物滤池对所述油田采出水进行分解和/或矿化处理以去除所述有机物。
  7. 根据权利要求6所述的方法，其中，在采用曝气生物滤池对所述油田采出水进行分解和/或矿化处理之前，还包括：对所述曝气生物滤池中的填料进行激活处理，其中，对所述曝气生物滤池中的填料进行激活处理包括：
    采用清水对所述曝气生物滤池进行冲洗，去除所述填料吸附的杂质和/或所述填料被磨损产生的粉末；
    采用氢氧化钠溶液处理所述填料，去除所述填料包括的有机物杂质，并采用清水对所述填料进行处理至中性；
    采用硫酸溶液处理所述填料，去除所述填料吸附的无机物，并采用清水对所述填料进行处理至中性。
  8. 根据权利要求7所述的方法，其中，所述曝气生物滤池中的填料包 括椰壳炭、杏壳炭和煤质活性炭中的至少之一。
  9. 根据权利要求6-8中任一项所述的方法，还包括：在所述曝气生物滤池中加入耐盐菌剂，其中，每立方米所述油田采出水中所述耐盐菌剂的质量为5～50g，且每克所述油田采出水中的所述耐盐菌剂中有效菌数大于或者等于2.0亿。
  10. 根据权利要求6-9中任一项所述的方法，还包括：采用超滤元件对所述曝气生物滤池出水进行超滤处理。
  11. 根据权利要求10所述的方法，还包括：采用反渗透元件对所述超滤元件出水进行反渗透处理以进行脱盐。
  12. 根据权利要求11所述的方法，还包括：采用树脂过滤器对经过所述反渗透处理后的浓水进行处理，其中，从所述树脂过滤器输出所述产水。
  13. 根据权利要求1-12中任一项所述的方法，其中，在对所述油田采出水进行降温和净化处理之前，还包括：对所述油田采出水进行预处理，
    所述预处理包括：采用调节池、氮气气浮单元、除硬除硅单元、沉淀池和过滤单元中的至少之一对所述油田采出水进行处理。
  14. 一种油田采出水的处理装置，包括：
    油田采出水提供部件，配置为提供油田采出水；
    换热部件，配置为对所述油田采出水进行降温处理；
    净化部件，配置为对进行降温处理后的所述油田采出水进行净化处理以得到产水；
    输水管，配置为输送所述产水，
    其中，所述换热部件的第一端与油田采出水提供部件相连，所述换热部件的第二端与所述输水管相连，使得所述油田采出水和所述产水在所述换热部件中进行热交换，以对所述油田采出水进行降温处理。
  15. 根据权利要求14所述的处理装置，其中，所述换热部件包括换热器。
  16. 根据权利要求14或15所述的处理装置，还包括散热器，其中，所述散热器配置为对所述油田采出水进行散热。
  17. 根据权利要求14-16中任一项所述的处理装置，还包括冷却塔，其中，所述冷却塔设置在所述换热部件和所述净化部件之间。
  18. 根据权利要求14-17中任一项所述的处理装置，其中，所述净化部 件包括氧化池、曝气生物滤池、超滤元件、反渗透元件和树脂过滤器中的至少之一。
  19. 根据权利要求18所述的处理装置，其中，所述氧化池包括电催化氧化部件，或者臭氧与双氧水的组合，或者电催化氧化部件和臭氧与双氧水的组合。
  20. 根据权利要求18或19所述的处理装置，其中，所述曝气生物滤池中的填料为椰壳炭、杏壳炭和煤质活性炭中的至少之一。
  21. 根据权利要求14-20中任一项所述的处理装置，还包括预处理部件，其中，所述预处理部件包括调节池、氮气气浮单元、除硬除硅单元、沉淀池和过滤单元中的至少之一。
  22. 根据权利要求21所述的处理装置，其中，所述过滤单元包括覆膜纤维球过滤器和管式微滤膜过滤器。
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