CN111039434A - Oily sewage treatment process and system - Google Patents
Oily sewage treatment process and system Download PDFInfo
- Publication number
- CN111039434A CN111039434A CN201911303636.2A CN201911303636A CN111039434A CN 111039434 A CN111039434 A CN 111039434A CN 201911303636 A CN201911303636 A CN 201911303636A CN 111039434 A CN111039434 A CN 111039434A
- Authority
- CN
- China
- Prior art keywords
- treatment
- mixture
- sewage
- coalescence
- oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention provides an oily sewage treatment process, which comprises the following steps: carrying out dissolved air flotation treatment on oily sewage to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage. The process carries out primary demulsification on emulsified oil of oily sewage through dissolved air floatation treatment, so that an oil-water two-phase interface is clearer; then, filtering treatment is carried out to effectively remove most suspended substances and part of emulsified oil in the oily sewage; further carry out the complete breakdown of emulsion with emulsified oil and super emulsified oil through coalescence deoiling processing, realize profit quickly separating, carry out the coalescence to highly emulsified oil simultaneously, reach simultaneously effective, the stable effect that realizes emulsified oil breakdown of emulsion and suspended solid and get rid of.
Description
Technical Field
The invention relates to the field of sewage treatment, in particular to a process and a system for treating oily sewage.
Background
Can produce a large amount of oil contents height in the petroleum and petrochemical industry production process, the emulsification is serious, carry a large amount of slight suspended solid oily sewage, and this sewage oil content is the highest, and the emulsified oil particle size is little (most all is below 20 um), and the emulsified oil parcel forms stable emulsified oily sewage on the suspended solid surface simultaneously, subsides unable layering for a long time, leads to the unable satisfied requirement of conventional processing technology. The milk treatment effect is not good, gets into low reaches processing apparatus, causes low reaches device to block up easily, influences the operation effect, leads to the unable normal operating of device when serious, needs the shutdown maintenance, causes very big difficulty for low reaches sewage treatment plant.
The treatment process of the oily sewage in the prior art comprises the steps of gravity settling, cyclone centrifugal separation, ceramic membrane filtration, coalescence demulsification separation process and the like, and specifically comprises the following steps:
the gravity settling process usually has settling time from 40 hours to 800 hours, and the settling time is 50-70 hours. But because the oil-containing emulsification is serious, the coke powder particles are small, even if the coke powder particles are settled for a long time, the separation effect is still not obvious, meanwhile, the occupied area is large, the capital construction cost is high, the investment is large, in addition, because the settling tank is in an open or semi-closed state, acid gas leaks out, the surrounding environment and the health of staff are seriously influenced, and the current environmental protection requirement is not met.
Although the cyclone centrifugal separation process is improved by heavy force sedimentation, the cyclone effect is still very limited because the emulsified oil has small particle size and very close density to water, and the effects of removing oil and suspended matters are still not obvious. Meanwhile, the process has poor impact resistance, unstable oil removal effect and easy blockage of the cyclone, and even can not work normally in severe cases.
The ceramic membrane is taken as a core equipment treatment process, although the membrane has high filtration precision and good short-term effluent and can meet the requirements, the process has large investment, high operation and maintenance cost, easy membrane blockage and poor stability, and simultaneously generates a large amount of concentrated water and waste liquid generated by acid washing and alkali washing during regeneration, thereby having secondary pollution.
The coalescence demulsification separation requires that most fine suspended matters need to be removed before coalescence demulsification, otherwise, the coalescer is easy to block, and the coalescer fails due to perforation. If coarse filtration with low accuracy is selected, the coalescer is easily blocked and fails, and the coalescer cannot stably operate for a long time.
In the step of treating the oily sewage based on the existing method, emulsion breaking and suspended matter removal of the emulsified oil cannot be simultaneously and effectively and stably realized under the condition that the emulsified oil and the fine suspended matter are mutually wrapped.
Disclosure of Invention
The invention aims to provide an oily sewage treatment process and system, and aims to solve the problem that emulsion breaking and suspended matter removal of emulsified oil cannot be simultaneously and effectively and stably realized under the condition that emulsified oil and fine suspended matters are mutually wrapped by the existing sewage treatment process.
In order to achieve the purpose, the invention adopts the following technical scheme:
a process for treating oily sewage comprises the following steps:
carrying out dissolved air flotation treatment on oily sewage to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
And, an oily sewage treatment system comprising, connected in sequence: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus.
The oily sewage treatment process of the invention is to treat oily sewage by a process of 'dissolved air flotation treatment, filtration treatment and coalescent oil removal treatment', firstly, the oily sewage is firstly treated by the dissolved air flotation treatment, in the dissolved air flotation treatment process, a large amount of highly dispersed micro-nano bubbles are introduced into the oily sewage to be treated to be used as carriers to be adhered to particles (oil drops) or floccules suspended in water to form floating bodies with integral density smaller than that of the water, and the floating bodies float to the water surface by the buoyancy action to form floating oil for removal, so that most of emulsified oil and fine suspended matters in the oily sewage are removed, the burden of the subsequent filtration treatment step and the coalescent oil removal treatment step is greatly reduced, the backwashing frequency in the filtration step can be greatly reduced, the backwashing water yield is reduced, the filtration water yield is improved, and the blockage period of a filter and a coalescer is greatly delayed, creating conditions for subsequent processing steps.
And secondly, performing filtration treatment, wherein the filtration treatment step is mainly used for removing most suspended substances in the first mixture subjected to dissolved air floatation treatment, removing solid substances in the oily sewage, and providing sewage with low solid content for the subsequent coalescence deoiling treatment step, so that the coalescence deoiling treatment effect is good.
And finally, performing coalescence deoiling treatment, wherein the coalescence deoiling treatment mainly comprises the step of coalescing the second mixture with low solid content to remove emulsified oil in water, in the coalescence treatment process of the sewage containing the emulsified oil, oil drops in an emulsified state and an ultra-emulsified state are coalesced into larger oil drops, and the large oil drops are coalesced into large oil masses to realize quick separation so as to achieve the deoiling effect.
The process carries out primary demulsification on emulsified oil of oily sewage through dissolved air floatation treatment, so that an oil-water two-phase interface is clearer; then, filtering treatment is carried out to effectively remove most suspended matters and part of emulsified oil in the oily sewage, thereby creating favorable conditions for subsequent coalescence and oil removal; further carry out the complete breakdown of emulsion with emulsified oil and super emulsified oil through coalescence deoiling processing, realize profit quickly separating, carry out the coalescence to highly emulsified oil simultaneously, reach simultaneously effective, the stable effect that realizes emulsified oil breakdown of emulsion and suspended solid and get rid of. The process has few steps and short treatment time, and is favorable for being applied to the treatment process of high-emulsification oil-containing and solid-containing sewage such as coking acid water, gas field condensate water, steam condensate water and the like.
The invention relates to an oily sewage treatment system, which comprises: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus.
The invention takes the dissolved air flotation device, the filtering device and the coalescence deoiling processing device as the oily sewage processing system to realize the processing of the oily sewage by adopting the processes of the dissolved air flotation processing, the filtering processing and the coalescence deoiling processing.
Drawings
FIG. 1 is a process flow diagram provided by an embodiment of the present invention.
FIG. 2 is a process flow diagram provided by an embodiment of the present invention.
Fig. 3 is a schematic structural diagram of a rotational flow dissolved air flotation device according to an embodiment of the present invention.
Fig. 4 is a schematic structural diagram of a rotational flow generating device of the rotational flow dissolved air flotation device according to the embodiment of the present invention.
Fig. 5 is a schematic structural diagram of a coalescing oil removal processing device (a plurality of vertical coalescing cores) provided by an embodiment of the invention.
Fig. 6 is a schematic structural diagram of a coalescing oil removal processing apparatus (a plurality of horizontal coalescing cores) provided in an embodiment of the present invention.
Fig. 7 is a schematic diagram of the operation process of the coalesced oil removal processing device provided by the embodiment of the invention.
FIG. 8 is a sample of oily wastewater and treated wastewater from day one (4 months and 14 days) afternoon at 16:00 as provided in example 1 of the present invention.
FIG. 9 is a sample of oily wastewater and treated wastewater at 10:00 am the next day (day 4 and 15) as provided in example 1 of the present invention.
FIG. 10 is a sample of oily wastewater and treated wastewater at 15:00 PM the next day (4 months and 15 days) as provided in example 1 of the present invention.
FIG. 11 is a sample of oily wastewater and treated wastewater at 10:00 am on the third day (day 4 and day 16) as provided in example 1 of the present invention.
FIG. 12 is a sample of oily sewage and treated sewage at 15:00 PM on the third day (day 4 and day 16) as provided in example 1 of the present invention.
Detailed Description
In order to make the objects, technical solutions and technical effects of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments obtained by a person of ordinary skill in the art without any inventive step in connection with the embodiments of the present invention shall fall within the scope of protection of the present invention.
In the description of the present invention, it is to be understood that the terms "first", "second" and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
The embodiment of the invention provides an oily sewage treatment process, which comprises the following steps:
s01, carrying out dissolved air floatation treatment on the oily sewage to obtain a first mixture;
s02, filtering the first mixture to obtain a second mixture;
and S03, performing coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
The oily sewage treatment process of the invention is to treat oily sewage by a process of 'dissolved air flotation treatment, filtration treatment and coalescent oil removal treatment', firstly, the oily sewage is firstly treated by the dissolved air flotation treatment, in the dissolved air flotation treatment process, a large amount of highly dispersed micro-nano bubbles are introduced into the oily sewage to be treated to be used as carriers to be adhered to particles (oil drops) or floccules suspended in water to form floating bodies with integral density smaller than that of the water, and the floating bodies float to the water surface by the buoyancy action to form floating oil for removal, so that most of emulsified oil and fine suspended matters in the oily sewage are removed, the burden of the subsequent filtration treatment step and the coalescent oil removal treatment step is greatly reduced, the backwashing frequency in the filtration step can be greatly reduced, the backwashing water yield is reduced, the filtration water yield is improved, and the blockage period of a filter and a coalescer is greatly delayed, creating conditions for subsequent processing steps.
And secondly, performing filtration treatment, wherein the filtration treatment step is mainly used for removing most suspended substances in the first mixture subjected to dissolved air floatation treatment, removing solid substances in the oily sewage, and providing sewage with low solid content for the subsequent coalescence deoiling treatment step, so that the coalescence deoiling treatment effect is good.
And finally, performing coalescence deoiling treatment, wherein the coalescence deoiling treatment mainly comprises the step of coalescing the second mixture with low solid content to remove emulsified oil in water, in the coalescence treatment process of the sewage containing the emulsified oil, oil drops in an emulsified state and an ultra-emulsified state are coalesced into larger oil drops, and the large oil drops are coalesced into large oil masses to realize quick separation so as to achieve the deoiling effect.
Specifically, in step S01, the oily sewage is subjected to dissolved air flotation to obtain a first mixture. In the dissolved air flotation treatment process, a large amount of highly dispersed micro-nano bubbles are introduced into oily sewage to be treated, the micro-nano bubbles are used as carriers to be adhered to particles (oil drops) or floccules suspended in water to form a floating body with integral density smaller than that of water, and the floating body floats to the water surface under the action of buoyancy to form floating oil for removal, so that most of emulsified oil and fine suspended matters in the oily sewage are removed, the burden of a subsequent filtration treatment step and a coalescence oil removal treatment step are greatly reduced, the backwashing frequency in the filtration step can be greatly reduced, the backwashing water yield is reduced, the filtration water yield is improved, the blockage period of a filter and a coalescer is greatly delayed, and conditions are created for the subsequent treatment step.
Preferably, in the step of obtaining the first mixture by carrying out dissolved air floatation treatment on the oily sewage, a dissolved air floatation device is adopted for treatment, and the treatment time of the dissolved air floatation treatment is 1-10 minutes. Preferably, the dissolved air flotation device is a device which is simultaneously provided with a cyclone centrifugal separation assembly and a dissolved air flotation separation assembly. The dissolved air flotation device firstly utilizes the technology of partial reflux air flotation, the effluent and the gas of the device are sucked by a cyclone dissolved air pump, the liquid and the gas are mixed by a pump impeller rotating at high speed, the gas is fully dissolved in the liquid, and the dissolving efficiency can reach more than 95 percent. Meanwhile, an internal part is arranged in the dissolved gas tank, so that gas is contacted with water components to further improve the dissolved gas efficiency. Water containing micro bubbles (with the particle size of 5-30 microns) enters a high-efficiency rotational flow air flotation inlet pipeline and is mixed with inlet water, then enters a dissolved air flotation device from the bottom in a tangential mode, weak rotational flow is generated at the bottom, on one hand, oil drops and the micro-nano bubbles are transported to the center of the container through the weak rotational flow, on the other hand, the collision adhesion between the oil drops and the micro-nano bubbles is promoted to be strengthened, then the air flotation effect is generated, the multiphase mixture of the oil drops, the bubbles, suspended matters and the water floating to the liquid level is discharged from the top of the container by means of pressure, and the treated. The oil-containing sewage has the comprehensive effects of cyclone centrifugal separation and dissolved air floatation separation in the dissolved air floatation device, and the effect is far higher than the effects of independent cyclone and air floatation, so that higher efficiency can be achieved in a short treatment time.
Preferably, the treatment time of the dissolved air floatation treatment is 1-10 minutes. The treatment time of the dissolved air floatation treatment is controlled to be short, and the dissolved air floatation treatment of the oily sewage is ensured to be completed within 1-10 minutes.
Preferably, in the step of obtaining the first mixture by carrying out dissolved air flotation treatment on the oily sewage, the system pressure difference of the dissolved air flotation treatment is 0.05-0.06 Mpa, and the treatment pressure is 0.05-0.3 Mpa, and the system pressure difference and the treatment pressure of the dissolved air flotation treatment are controlled, so that moderate pressure can be ensured in the treatment process of the oily sewage, large-particle solid impurities in the oily sewage can be removed, the service life of the oily sewage can be ensured, and the equipment cannot be damaged due to overlarge pressure.
Preferably, in the step of obtaining the first mixture by carrying out dissolved air flotation treatment on the oily sewage, the treatment temperature of the dissolved air flotation treatment is 0-85 ℃, if the treatment temperature is too low, the viscosity of the oily sewage is increased, the contact of bubbles with suspended matters and oil drops is increased, the treatment effect is further influenced, and the separation effect of the oil drops, the suspended matters and the sewage is poor; if the treatment temperature is too high, the content of dissolved gas in the dissolved gas water is reduced, so that the number of micro bubbles is insufficient, the air floatation effect is influenced, and the separation effect of oil drops, suspended matters and sewage is poor. In the preferred embodiment of the invention, the treatment temperature of the dissolved air floatation treatment is 30-60 ℃, and under the temperature condition, suspended substances and oil drops in the oily sewage are combined with micro-bubbles, so that the air floatation effect is high, and the good separation effect is ensured.
Preferably, in the step of subjecting the oily sewage to dissolved air flotation treatment to obtain the first mixture, the oily sewage is treated by a rotational flow dissolved air flotation treatment method.
In the specific embodiment of the invention, the specific operation method for obtaining the first mixture by carrying out dissolved air flotation treatment on the oily sewage by adopting the rotational flow air flotation device is as follows: introducing oily sewage into a cyclone air flotation device (CDFU device), and controlling the diameter of a large amount of ultramicro bubbles released by a mixing device and dissolved gas water to be 5-30 mu m; mixing the sewage containing the sewage and the ultramicro bubbles, then tangentially entering a dissolved air floatation tank along the wall of a CDFU tank, quickly forming a uniform rotational flow field with certain strength under the action of tangential power flow and an internal fluid component, quickly colliding and adhering a large amount of ultramicro bubbles and emulsified oil drops under the action of centrifugal force generated by rotational flow, gathering the ultramicro bubbles and the emulsified oil drops to form floating oil, gradually floating up, entering an oil collecting inner cylinder, and then discharging the floating oil into a floating oil collecting system through an oil discharge port; and (4) discharging separated waste gas after flotation into a waste gas treatment system through a gas outlet at the top of the air flotation to obtain a first mixture.
Specifically, in step S02, the first mixture is filtered to obtain a second mixture; the filtering treatment step is mainly used for removing most suspended substances in the first mixture after dissolved air floatation treatment, removing solid substances in the oily sewage, providing sewage with low solid content for the subsequent coalescence deoiling treatment step and ensuring that the coalescence deoiling treatment effect is good.
Preferably, in the step of filtering the first mixture to obtain the second mixture, the first mixture is filtered under the condition that the absolute filtration precision is less than or equal to 10 μm. The filtering treatment is carried out under the condition that the absolute filtering precision is less than or equal to 10 mu m, so that large-particle impurities in the first mixture can be removed, the sewage with low solid content is provided for the subsequent coalescence oil-removing treatment step, and the coalescence oil-removing treatment effect is better. Because filtration treatment adsorbs the suspended solid and filters on filter media, and after the process, the adsorption of suspended solid can influence filter media's adsorption performance, and is preferred, will in the step that first mixture carries out filtration treatment and obtains the second mixture, including carrying out air water joint backwash step, carry out air water joint backwash step, can make the suspended solid of absorption in the filter media upwards float along with gas together in the liquid flushing process, more be favorable to getting rid of the suspended solid that adsorbs on filter media.
Preferably, the air-water combined backwashing method comprises the following steps: after air washing for 5 s-5 min, washing for 1 min-30 min; repeating the steps of air washing and water washing for 2-3 times. Firstly, the suspended matter is dispersed by adopting a gas washing mode, so that the adhesion of the suspended matter and a filter medium is poor; and then the suspended matters are washed by using a water washing mode to remove the suspended matters in the filter medium. Wherein, the air washing is carried out for 5 s-5 min, and if the air washing time is too short, the suspended matters can not be dispersed, so that the suspended matters still have strong adhesion with the filter medium and are not easy to remove; and then washing for 1-30 min, wherein if the washing time is too short, the suspended matters cannot be washed clean, and if the washing time is too long, the reaction efficiency is affected.
Further preferably, the air-water combined backwashing method comprises the following steps: after air washing for 5 s-5 min, washing for 1 min-30 min; repeating the steps of air washing and water washing for 2-3 times. Repeating the above cleaning cycle for 2-3 times. Repeating the cleaning cycle for 2-3 times to clean the suspended matters.
Preferably, in the air-water combined backwashing step, the pressure difference is controlled to be 0.01MPa to 0.1 MPa. The differential pressure is controlled to be 0.01 MPa-0.1 MPa, the air-water combined backwashing process can be realized in the filtering process, the pressure is moderate, and most of suspended matters can be removed. In the preferred embodiment of the invention, the pressure difference is 0.03MPa to 0.05MPa, which can ensure that most suspended matters are removed, and can ensure the service life of the device, and can ensure that the device is not damaged due to overlarge pressure.
Specifically, in step S03, the second mixture is subjected to coalescing degreasing treatment to obtain degreasing and desmutting sewage. The coalescence deoiling treatment is mainly to coalesce the second mixture with low solid content to remove emulsified oil in water, in the process of coalescence treatment of sewage containing emulsified oil, oil drops in an emulsification state and a super-emulsification state are coalesced into larger oil drops, and the large oil drops are coalesced into large oil masses to realize quick separation, so as to achieve the deoiling effect.
Preferably, in the step of performing coalesced oil removal treatment on the second mixture to obtain oil-removed and solid-removed sewage, the system pressure difference of the coalesced oil removal treatment is 0.01-0.2 MPa, so that moderate pressure is ensured in the coalesced oil removal treatment process, and the oil removal effect can be ensured.
Preferably, in the step of performing coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage, the treatment temperature of the coalescence deoiling treatment is 0-85 ℃. If the treatment temperature is too low, the viscosity of the dirty oil is too high, when the viscosity is more than 50mpas, the oil coalesced on the coalescing core cannot be separated, the oil is adhered on the filter core, the filter core is damaged, the demulsification effect cannot be achieved, and the oil removal effect cannot be achieved; if the temperature is too high, the physical properties of the filter element material are changed, and the oil removing effect cannot be ensured.
Preferably, in the step of performing coalesced oil removal treatment on the second mixture to obtain oil-removed and solid-removed sewage, the treatment time of the coalesced oil removal treatment is 10-60 minutes. If the treatment time is too short, the oil removal effect cannot be completely realized; if the treatment time is too long, the treatment efficiency is low, and the treatment efficiency is impaired. In the specific embodiment of the invention, a coalescence deoiling device is selected to carry out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
Preferably, before the step of subjecting the oily sewage to dissolved air flotation treatment to obtain the first mixture, the method further comprises the step of subjecting the oily sewage to coarse filtration treatment. Before dissolved air flotation treatment, the oily sewage is subjected to coarse filtration treatment, so that large-particle solid impurities in the oily sewage are removed, and the subsequent treatment steps are convenient to perform.
Preferably, in the step of coarse filtration treatment, filter screen with aperture of 10 ~ 100um is selected for use and is filtered, and the purpose is in order to make solid impurity removal that particle is big such as coke breeze, suspended solid. If the pore diameter is too large, the filtering effect cannot be achieved; if the pore diameter is too small, the filtration accuracy of the coarse filtration becomes too high, and the life of the coarse filter becomes short. In the preferred embodiment of the invention, in the step of the coarse filtration treatment, a filter screen with the aperture of 20-50 μm is selected for filtration, and the filter screen with the aperture is adopted for filtration, so that solid impurities with larger particles can be better removed.
Preferably, the step of the coarse filtration treatment further comprises a backwashing step. Preferably, in the backwashing step, the backwashing differential pressure is controlled to be 0.01 to 0.1MPa, and if the backwashing differential pressure is too small, the backwashing frequency is high and the efficiency is low; if the backwash pressure difference is too large, the cost is high. Meanwhile, if the backwashing pressure difference is too large, the filter membrane is easily damaged, and the service life of the filter membrane is influenced; and easily cause too big suspended solid to get into in the filter membrane pore, lead to the filter membrane jam, influence the backwash effect. In a preferred embodiment of the invention, in the backwashing step, the backwashing differential pressure is controlled to be 0.013 MPa-0.05 MPa, and backwashing is performed under the differential pressure condition, so that large-particle solid impurities in the oily sewage can be removed, the filter is not easily blocked, and the backwashing effect is excellent.
In some embodiments, when the content of suspended matters in the oily sewage is not less than 300mg/L and the particle size of solid impurities in the oily sewage is 10-100 um, the method further comprises a step of performing coarse filtration treatment on the oily sewage before the step of performing dissolved air flotation treatment on the oily sewage to obtain a first mixture. As shown in the process flow chart of FIG. 1, the process for treating oily sewage comprises the following steps: carrying out coarse filtration treatment on the oily sewage, and carrying out rotational flow dissolved air floatation treatment on the oily sewage obtained by the coarse filtration treatment to obtain a first mixture; carrying out precision filtration treatment on the first mixture to obtain a second mixture; carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage;
wherein the system pressure difference of the rotary-floating dissolved air floatation treatment is 0.05Mpa to 0.06Mpa, the treatment pressure is 0.05Mpa to 0.3Mpa, the treatment temperature is 0 ℃ to 85 ℃, and the treatment time is 1 to 10 minutes;
the coarse filtration treatment and the precise filtration treatment both comprise a gas-water combined backwashing step, the pressure difference is controlled to be 0.01 MPa-0.1 MPa, and the gas-water combined backwashing method comprises the following steps: after air washing for 5 s-5 min, washing for 1 min-30 min; repeating the steps of air washing and water washing for 2-3 times;
the system pressure difference of the coalescence deoiling treatment is 0.01 MPa-0.2 MPa, the treatment temperature is 0-85 ℃, and the treatment time is 10-60 minutes.
In some embodiments, when the content of suspended matters in the oily sewage is less than 300mg/L and the particle size of solid impurities in the oily sewage is more than 10um, the oily sewage does not need to be subjected to coarse filtration treatment before the step of subjecting the oily sewage to dissolved air flotation treatment to obtain the first mixture. As shown in the process flow chart of FIG. 2, the process for treating oily sewage comprises the following steps: subjecting the oily sewage to rotary-floating dissolved air flotation treatment to obtain a first mixture; carrying out precision filtration treatment on the first mixture to obtain a second mixture; carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage;
wherein the system pressure difference of the rotary-floating dissolved air floatation treatment is 0.05Mpa to 0.06Mpa, the treatment pressure is 0.05Mpa to 0.3Mpa, the treatment temperature is 0 ℃ to 85 ℃, and the treatment time is 1 to 10 minutes;
the precise filtration treatment comprises a step of air-water combined backwashing, the pressure difference is controlled to be 0.01 MPa-0.1 MPa, and the air-water combined backwashing method comprises the following steps: after air washing for 5 s-5 min, washing for 1 min-30 min; repeating the steps of air washing and water washing for 2-3 times;
the system pressure difference of the coalescence deoiling treatment is 0.01 MPa-0.2 MPa, the treatment temperature is 0-85 ℃, and the treatment time is 10-60 minutes. The process carries out primary demulsification on emulsified oil of oily sewage through dissolved air floatation treatment, so that an oil-water two-phase interface is clearer; then, filtering treatment is carried out to effectively remove most suspended matters and part of emulsified oil in the oily sewage, thereby creating favorable conditions for subsequent coalescence and oil removal; further carry out the complete breakdown of emulsion with emulsified oil and super emulsified oil through coalescence deoiling processing, realize profit quickly separating, carry out the coalescence to highly emulsified oil simultaneously, reach simultaneously effective, the stable effect that realizes emulsified oil breakdown of emulsion and suspended solid and get rid of. The process has few steps and short treatment time, and is favorable for being applied to the treatment process of high-emulsification oil-containing and solid-containing sewage such as coking acid water, gas field condensate water, steam condensate water and the like.
Correspondingly, the embodiment of the invention also provides an oily sewage treatment system, which comprises the following components in sequence: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus.
The invention relates to an oily sewage treatment system, which comprises: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus. The invention takes the dissolved air flotation device, the filtering device and the coalescence deoiling processing device as the oily sewage processing system to realize the processing of the oily sewage by adopting the processes of the dissolved air flotation processing, the filtering processing and the coalescence deoiling processing.
Preferably, the dissolved air flotation device is a rotational flow dissolved air flotation device, as shown in fig. 3, the rotational flow dissolved air flotation device comprises a sealable tank body 1, a dirty oil outlet 8 is formed in the top of the tank body, a treated water outlet 10 is formed in the bottom of the tank body, an inner cylinder 5 is arranged in the tank body 1, the inner cylinder 5 and the tank body 1 are coaxially arranged, an air-liquid mixed sewage inlet pipe is communicated with the bottom of the inner cylinder, a rotational flow generating device 7 is arranged in the inner cylinder, and a porous rectifying plate 6 is further arranged between the rotational flow generating device and the bottom of the inner cylinder. The inner cylinder 5 has an open top, an opening 52 in the shape of an inverted trumpet, a cylindrical middle 51, and a tapered bottom 53. An annular baffle 9 is arranged along the outer wall of the inner cylinder, the baffle inclines downwards, and a gap is reserved between the baffle and the inner wall of the tank body. The gas-liquid mixed sewage inlet pipe is connected with the sewage inlet pipe 2 and the gas-liquid mixed inlet pipe 3 through a mixer 4, and the tank body of the rotational flow dissolved air floatation device is divided into a cylinder inner area 102 and a cylinder outer area 103 by an inner cylinder. As shown in fig. 4, the swirling flow generating device 7 includes a center post 71 and a deflector 72 rotating around the center post.
The working process of the rotational flow dissolved air flotation device is as follows: oily sewage enters through the sewage inlet pipe 2, is mixed with gas-liquid mixed liquid carrying a large number of micro bubbles in the gas-liquid mixed inlet pipe 3 through the mixer 4, enters the bottom of the inner cylinder 5 through the gas-liquid mixed sewage inlet pipe, flows upwards through the porous rectifying plate 6, enters the rotational flow generating device 7, generates rotational flow under the action of the flow deflector 71 between the inner cylinder 3 and the central column 72, micro bubbles carry oil drops to gradually move towards the middle of the inner cylinder area 101 and ascend to a gas-liquid interface 102, bubbles are separated out, and the oil drops form scum which is discharged through a dirty oil outlet 8 or an oil outlet 12. Meanwhile, the sewage after flotation moves downwards to the area 103 outside the inner cylinder 5 after overflowing the inverted bell mouth 52 of the inner cylinder, bypasses the inclined baffle 4 and is discharged through the treated water outlet 10.
The cyclone dissolved air flotation device tank body is divided into an inner cylinder area and an outer cylinder area by the inner cylinder, the flotation area is divided into a plurality of functional areas, the internal flow field of the flotation is refined, the flow path of the dirty oil and the treated sewage is separated, oil drops are prevented from being carried away by the treated water, the oil content of an outlet is reduced, and the separation efficiency is higher. Meanwhile, the device has the advantages of more reasonable internal flow field organization, higher space utilization rate and more compact container structure. Secondly, the rotational flow generating device is arranged at the bottom of the inner cylinder, so that a larger rotating speed can be generated, a larger centrifugal acceleration can be obtained, oil drops can be promoted to be quickly coalesced to the middle of the inner cylinder, the retention time is shortened, the structure is more compact, the rotational flow generated by the rotational flow generating device is more stable, the flow field is more uniform, the air floatation effect is more facilitated, and the oil removing efficiency is improved; moreover, an annular baffle is installed on treated water outlet upper portion, plays and relaxes the rivers for treated water outlet rivers are more even mild, prevent that outlet water from carrying silt, reduce outlet aquatic oil content, improve separation efficiency. The cyclone dissolved air flotation device is a device combining a cyclone centrifugal separation technology and a dissolved air flotation separation technology, the internal flow field structure is more reasonable, the generated centrifugal strength is higher, the structure is more compact, and better oil removal and sand removal effects can be obtained.
Preferably, the coalescence deoiling processing apparatus is a horizontal structure, and comprises a tank body, and the tank body space is divided into an emulsification coalescence demulsification area, a fluid stabilization area, a liquid-liquid coalescence packing area and a liquid-liquid separation area from left to right in sequence.
Preferably, an emulsion coalescence demulsifying area is arranged, two-phase emulsion of the immiscible liquid to be separated firstly enters the coalescence demulsifying area, the coalescence demulsifying area consists of a single or a plurality of coalescence demulsifying filter elements made of special materials, when the liquid state passes through the coalescence demulsifying filter elements, droplets of the emulsified discrete liquid phase and the ultra-emulsified discrete liquid phase are captured and coalesced into large droplets by micro-nano fibers on the filter elements, and meanwhile, the free liquid phase directly enters the fluid stabilizing area through the coalescence demulsifying filter elements. Preferably, the coalescence demulsification area consists of a nanofiber coalescence demulsification filter element. Furthermore, the coalescence core is a single coalescence core or a plurality of coalescence cores, and the arrangement mode is vertical or horizontal. As shown in FIG. 5, the coalesced oil removing treatment device is provided with a plurality of vertical coalesced cores. As shown in FIG. 6, the coalesced oil removing treatment device is provided with a plurality of horizontal coalesced cores.
Preferably, the fiber coalescence core is woven by a large number of micro-nano superfine fiber yarns, and the superfine fiber material is selected from one or more of metal fibers, glass fibers, polytetrafluoroethylene fibers, polypropylene fibers, polyester fibers and the like. In a preferred embodiment of the present invention, the ultrafine fiber material is selected from at least one of polytetrafluoroethylene, polyester fiber, and polypropylene fiber. Further preferably, the fiber can be modified or surface-coated, so that the fiber surface has super-hydrophilicity, super-lipophilicity or super-lipophilicity and non-hydrophilicity, so as to better demulsify and separate the liquid-liquid two-phase emulsified state and the super-emulsified state.
Preferably, a porous flow stabilizing plate is arranged in the fluid stabilizing area; further preferably, the flow stabilizer is a single flow stabilizer or a plurality of flow stabilizers. The arrangement of the flow stabilizing plate mainly ensures that the fluid is in a laminar flow state quickly, the liquid carrying large liquid drops after coalescence quickly eliminates kinetic energy through the porous flow stabilizing plate, and the fluid enters the liquid coalescence packing area after the fluid is in the laminar flow state quickly.
Preferably, the liquid-liquid coalescence packing area is provided with a special efficient coalescence-separation packing; the liquid carrying the large liquid drops enters a coalescence filler area in a laminar flow state, and under the action of the coalescence filler, the large liquid drops are rapidly gathered and polymerized into liquid masses or even continuous liquid phases and then enter a liquid-liquid separation area. Further preferably, the coalescent packing is selected from any one of corrugated packing, inclined plate packing, inclined tube packing, and special corrugated packing. More preferably, the thickness of the filler is 200mm to 4000 mm.
Preferably, the liquid-liquid separation zone has the functions that the separated liquid forms a large liquid mass after demulsification and coalescence, and the light component large liquid mass quickly floats upwards under the action of buoyancy to form a component-philic liquid layer and is discharged from the liquid collection bag at the top; heavy components sink rapidly under the action of gravity to form a heavy component liquid layer, the heavy component liquid layer is discharged from a bottom outlet, and the liquid phase with lighter density is discharged from a top liquid collecting bag.
The operation process of the coalescence deoiling processing device is shown in fig. 7, the sewage containing the emulsification oil firstly enters the coalescence demulsification filter element through an inlet, and in the process of passing through the coalescence core, the emulsification state oil drops and the super-emulsification state oil drops are captured by the micro-nano fibers on the filter element and coalesced into larger oil drops (free oil drops) and then reach a fluid stable region; under the action of a porous flow stabilizing plate, the sewage flow state is quickly in a laminar flow state, stable fluid conditions are provided for rear-end coalescence, the sewage in the laminar flow state enters a special efficient coalescence separation filler, under the action of the coalescence filler, large liquid drops after demulsification are quickly aggregated and polymerized into an oil mass or an oil layer, and then enter an oil-water-liquid separation region; separating the oil mass or oil layer in the liquid-liquid separation zone, quickly floating to the upper part of the separator tank to form an oil layer, and then discharging from the top liquid collection bag; the sewage rapidly sinks into the sewage layer and then is discharged from the bottom outlet. Preferably, the oily sewage treatment system further comprises a coarse filtering device, and the coarse filtering device is arranged at one end of the dissolved air floatation device, which is far away from the filtering device. The purpose of the coarse filter device is to remove large solid impurities such as coke powder, suspended matters and the like.
In some embodiments, when the content of suspended matters in the oily sewage is more than or equal to 300mg/L and the particle size of solid impurities in the oily sewage is 10-100 um, in the oily sewage treatment system, the oily sewage treatment system comprises: a coarse filtration device, a dissolved air flotation device, a filtration device and a coalescence deoiling treatment device. Preferably, the treatment process of the oily sewage comprises the following steps: carrying out coarse filtration treatment on the oily sewage, and carrying out dissolved air floatation treatment on the oily sewage obtained by the coarse filtration treatment to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
In some embodiments, when the content of suspended matter in the oily sewage is less than 300mg/L, and the particle size of solid impurities in the oily sewage is more than 10um, the oily sewage treatment system comprises: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus. Preferably, the treatment process of the oily sewage comprises the following steps: carrying out dissolved air flotation treatment on the oily sewage to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
The details of the following examples are further described below.
Example 1
Coking acidic water treatment test of medium petrochemical Luoyang division
The oily sewage treatment process disclosed by the invention is adopted to carry out treatment tests on coking acidic water of the petrochemical Luoyang division company in the year 2019 from 14 days in the year 4 to 16 days in the year 2019 in the year 4, and the test processes are as follows:
the method comprises the following steps of treating oily sewage by taking coking acidic oily sewage of a Luoyang petrochemical company as a test object, wherein the color of the sewage is milky super-emulsified oil, and the treatment process comprises the following steps:
carrying out dissolved air flotation treatment on oily sewage to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
The sewage was treated for 3 days, and the oil-containing sewage and the sewage obtained by the treatment were collected at 16:00 pm on the first day (4 months and 14 days), 10:00 am on the second day (4 months and 15 days), 15:00 am on the second day (4 months and 15 days), 10:00 am on the third day (4 months and 16 days), and 15:00 am on the third day (4 months and 16 days), respectively, and the oil contents thereof were measured.
And (4) analyzing results:
the sewage was treated for 3 days while collecting and measuring the oil content of the oily sewage and the sewage obtained from the treatment for 16:00 pm on the first day (4 months and 14 days), 10:00 am on the second day (4 months and 15 days), 15:00 pm on the second day (4 months and 15 days), 10:00 am on the third day (4 months and 16 days), and 15:00 pm on the third day (4 months and 16 days), respectively, as shown in table 1:
the oil content of the oily sewage at 16:00 pm on the first day (4 months and 14 days) is 14800 mg/L; the oil content of the treated sewage is 46mg/L, and a sample is shown in FIG. 8, so that it can be found that the oil-containing sewage stock solution contains a large amount of milky super-emulsified oil and has high oil content; the sewage obtained after treatment basically does not contain milky super-emulsified oil, the oil content is low, and the water quality is oilless and transparent.
The oil content of the oily sewage at 10:00 am on the next day (4 months and 15 days) is 13750 mg/L; the oil content of the sewage obtained by treatment is 42 mg/L; as shown in FIG. 9, it can be found that the raw liquid of oily sewage contains a large amount of milky super-emulsified oil with high oil content; the sewage obtained after treatment basically does not contain milky super-emulsified oil, the oil content is low, and the water quality is oilless and transparent.
The oil content of the oily sewage at 15:00 pm in the next day (4 months and 15 days) is 23690 mg/L; the oil content of the sewage obtained by treatment is 51 mg/L; as shown in FIG. 10, it can be seen that the raw liquid of oily sewage contains a large amount of milky super-emulsified oil with high oil content; the sewage obtained after treatment basically does not contain milky super-emulsified oil, the oil content is low, and the water quality is oilless and transparent.
The oil content of the oily sewage at 10:00 am on the third day (4 months and 16 days) is 28000 mg/L; the oil content of the sewage obtained by treatment is 124 mg/L; as shown in FIG. 11, it can be found that the raw liquid of oily sewage contains a large amount of milky super-emulsified oil with high oil content; the sewage obtained after treatment basically does not contain milky super-emulsified oil, the oil content is low, and the water quality is oilless and transparent.
The oil content of the oily sewage at 15:00 pm on the third day (4 months and 16 days) is 26400 mg/L; the oil content of the sewage obtained by treatment is 85 mg/L; as shown in FIG. 12, it can be seen that the raw liquid of oily sewage contains a large amount of milky super-emulsified oil with high oil content; the sewage obtained after treatment basically does not contain milky super-emulsified oil, the oil content is low, and the water quality is oilless and transparent.
The process carries out primary demulsification on emulsified oil of oily sewage through dissolved air floatation treatment, so that an oil-water two-phase interface is clearer; then, filtering treatment is carried out to effectively remove most suspended matters and part of emulsified oil in the oily sewage, thereby creating favorable conditions for subsequent coalescence and oil removal; further carry out the complete breakdown of emulsion with emulsified oil and super emulsified oil through coalescence deoiling processing, realize profit quickly separating, carry out the coalescence to highly emulsified oil simultaneously, reach simultaneously effective, the stable effect that realizes emulsified oil breakdown of emulsion and suspended solid and get rid of. The process has the advantages of few steps and short treatment time, and achieves cost reduction and efficiency improvement while meeting the environmental protection requirement.
TABLE 1
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (10)
1. The oily sewage treatment process is characterized by comprising the following steps:
carrying out dissolved air flotation treatment on oily sewage to obtain a first mixture; filtering the first mixture to obtain a second mixture; and carrying out coalescence deoiling treatment on the second mixture to obtain deoiled and solid removed sewage.
2. The oily sewage treatment process according to claim 1, wherein in the step of subjecting the oily sewage to dissolved air floatation treatment to obtain the first mixture, a dissolved air floatation device is used for treatment, and the treatment time of the dissolved air floatation treatment is 1-10 minutes.
3. The oily sewage treatment process as claimed in claim 2, wherein in the step of subjecting the oily sewage to dissolved air floatation treatment to obtain the first mixture, the system pressure difference of the dissolved air floatation treatment is 0.05 Mpa-0.06 Mpa, the treatment pressure is 0.05 Mpa-0.3 Mpa, and the treatment temperature is 0 ℃ to 85 ℃.
4. The oily water treatment process according to claim 1, wherein in the step of subjecting the first mixture to filtration treatment to obtain the second mixture, the first mixture is subjected to filtration treatment under the condition that the absolute filtration accuracy is not more than 10 μm.
5. The oily water treatment process according to claim 4, wherein the step of filtering the first mixture to obtain the second mixture comprises a step of air-water combined backwashing on a filter subjected to the filtering treatment, and the air-water combined backwashing method comprises the following steps: after air washing for 5 s-5 min, washing for 1 min-30 min; repeating the steps of air washing and water washing for 2-3 times.
6. The oily sewage treatment process according to claim 5, wherein in the air-water combined backwashing step, the pressure difference is controlled to be 0.01MPa to 0.1 MPa.
7. The oily water treatment process according to any one of claims 1 to 6, wherein in the step of subjecting the second mixture to coalescence oil removal treatment to obtain oil-removed and solid-removed sewage, the system pressure difference of the coalescence oil removal treatment is 0.01MPa to 0.2MPa, and the treatment temperature is 0 ℃ to 85 ℃.
8. The oily sewage treatment process according to claim 7, wherein in the step of subjecting the second mixture to coalescence degreasing treatment to obtain degreased and solidified sewage, the treatment time of the coalescence degreasing treatment is 10-60 minutes.
9. An oily sewage treatment system, characterized in that, oily sewage treatment system includes in order the connection: dissolved air flotation device, filter equipment and coalescence deoiling processing apparatus.
10. The oily sewage treatment system of claim 9, wherein the dissolved air flotation device comprises a sealable tank body, the tank body is provided with a dirty oil outlet at the top and a treated water outlet at the bottom, an inner cylinder is arranged in the tank body, an air-liquid mixed sewage inlet pipe is communicated with the bottom of the inner cylinder, and a rotational flow generating device is arranged in the inner cylinder, wherein the rotational flow generating device comprises a central column and a flow deflector rotating around the central column; and/or the presence of a gas in the gas,
the coalescence deoiling processing device is of a horizontal structure and comprises a tank body, and the space of the tank body is sequentially divided into an emulsification coalescence demulsification area, a fluid stabilization area, a liquid-liquid coalescence packing area and a liquid-liquid separation area from left to right.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911303636.2A CN111039434A (en) | 2019-12-17 | 2019-12-17 | Oily sewage treatment process and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911303636.2A CN111039434A (en) | 2019-12-17 | 2019-12-17 | Oily sewage treatment process and system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111039434A true CN111039434A (en) | 2020-04-21 |
Family
ID=70237132
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911303636.2A Pending CN111039434A (en) | 2019-12-17 | 2019-12-17 | Oily sewage treatment process and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111039434A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112340867A (en) * | 2020-10-29 | 2021-02-09 | 重庆耐德环境技术有限公司 | Oily wastewater treatment device |
| CN112520921A (en) * | 2020-12-01 | 2021-03-19 | 华东理工大学 | Multi-physical-field-synergetic oily sewage treatment method and device |
| CN112624410A (en) * | 2020-12-17 | 2021-04-09 | 华东理工大学 | Deep purification method and device for oilfield produced water |
| CN113137195A (en) * | 2021-04-02 | 2021-07-20 | 安洁行方流体管理技术有限公司 | Recycling method and system for base liquid thrown out by oil-based drilling cuttings |
| CN113213648A (en) * | 2021-04-02 | 2021-08-06 | 安洁行方流体管理技术有限公司 | Oily sewage treatment method based on filtration and treatment system thereof |
| CN114455670A (en) * | 2022-01-18 | 2022-05-10 | 华东理工大学 | Oil refining sewage heterogeneous medium combined oil removing and suspension removing system and method |
| CN114538639A (en) * | 2022-01-18 | 2022-05-27 | 华东理工大学 | Pretreatment system and method for oily sewage before biochemical treatment |
| WO2022105698A1 (en) * | 2020-11-17 | 2022-05-27 | 华东理工大学 | Processing system and method for offshore gas field complex production fluid |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203440115U (en) * | 2013-06-27 | 2014-02-19 | 张力钧 | High-efficiency rotational flow air flotation device |
| CN103964545A (en) * | 2014-05-19 | 2014-08-06 | 华东理工大学 | Method and device for deep oil removal of wastewater containing low-concentration sump oil |
| CN203922875U (en) * | 2014-06-11 | 2014-11-05 | 深圳科力迩科技有限公司 | A kind of efficient coalescent oil-water separator |
| CN203922798U (en) * | 2014-06-11 | 2014-11-05 | 深圳科力迩科技有限公司 | A kind of coalescent pack for oily water separation |
| CN206434903U (en) * | 2016-09-19 | 2017-08-25 | 北京普思力科技有限公司 | A kind of oil-water separation system |
-
2019
- 2019-12-17 CN CN201911303636.2A patent/CN111039434A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203440115U (en) * | 2013-06-27 | 2014-02-19 | 张力钧 | High-efficiency rotational flow air flotation device |
| CN103964545A (en) * | 2014-05-19 | 2014-08-06 | 华东理工大学 | Method and device for deep oil removal of wastewater containing low-concentration sump oil |
| CN203922875U (en) * | 2014-06-11 | 2014-11-05 | 深圳科力迩科技有限公司 | A kind of efficient coalescent oil-water separator |
| CN203922798U (en) * | 2014-06-11 | 2014-11-05 | 深圳科力迩科技有限公司 | A kind of coalescent pack for oily water separation |
| CN206434903U (en) * | 2016-09-19 | 2017-08-25 | 北京普思力科技有限公司 | A kind of oil-water separation system |
Non-Patent Citations (2)
| Title |
|---|
| 王良均等: "《石油化工废水处理设计手册》", 31 May 1996, 中国石化出版社 * |
| 顾自立: "《现代电力企业物资管理》", 31 January 2007, 中国电力出版社 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112340867A (en) * | 2020-10-29 | 2021-02-09 | 重庆耐德环境技术有限公司 | Oily wastewater treatment device |
| WO2022105698A1 (en) * | 2020-11-17 | 2022-05-27 | 华东理工大学 | Processing system and method for offshore gas field complex production fluid |
| CN112520921A (en) * | 2020-12-01 | 2021-03-19 | 华东理工大学 | Multi-physical-field-synergetic oily sewage treatment method and device |
| CN112520921B (en) * | 2020-12-01 | 2023-07-25 | 华东理工大学 | Multi-physical-field cooperative oily sewage treatment method and device |
| CN112624410A (en) * | 2020-12-17 | 2021-04-09 | 华东理工大学 | Deep purification method and device for oilfield produced water |
| CN113137195A (en) * | 2021-04-02 | 2021-07-20 | 安洁行方流体管理技术有限公司 | Recycling method and system for base liquid thrown out by oil-based drilling cuttings |
| CN113213648A (en) * | 2021-04-02 | 2021-08-06 | 安洁行方流体管理技术有限公司 | Oily sewage treatment method based on filtration and treatment system thereof |
| CN114455670A (en) * | 2022-01-18 | 2022-05-10 | 华东理工大学 | Oil refining sewage heterogeneous medium combined oil removing and suspension removing system and method |
| CN114538639A (en) * | 2022-01-18 | 2022-05-27 | 华东理工大学 | Pretreatment system and method for oily sewage before biochemical treatment |
| CN114455670B (en) * | 2022-01-18 | 2024-01-26 | 华东理工大学 | Oil refining sewage foreign medium combined oil removal and suspension removal system and method |
| CN114538639B (en) * | 2022-01-18 | 2024-01-26 | 华东理工大学 | Pretreatment system and method for oily sewage before biochemical treatment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111039434A (en) | Oily sewage treatment process and system | |
| RU2505335C2 (en) | Method and device for multiphase fluid separation and their application | |
| CN112390420B (en) | System and method suitable for treating complex produced liquid of offshore gas field | |
| CN112520921B (en) | Multi-physical-field cooperative oily sewage treatment method and device | |
| EA021685B1 (en) | Apparatus and method for separation of phases in a multiphase flow | |
| CN201046371Y (en) | Oil-contaminated water purifying three-phase cyclone separator | |
| CN203763912U (en) | Three-phase separation device | |
| WO2015149196A1 (en) | Combination method and apparatus applying to three-phase separation | |
| CN103787527B (en) | A kind of oil-contaminated water air-float suspended layer filtration unit | |
| CN107522310A (en) | Not agent-feeding treatment oil-polluted water re-injection technique | |
| CN107983162B (en) | Membrane method oil-water separation device based on cyclone flushing | |
| CN112811667B (en) | Sequential oil removing system and method | |
| CN106241952A (en) | A kind of oil-water separation tower and oil-water separation method | |
| CN100457227C (en) | Rotational flow microporous filter | |
| CN212222478U (en) | Rotational flow air flotation oil removing device for delayed coking device | |
| Kajitvichyanukul et al. | Oil water separation | |
| CN203820565U (en) | Oily sewage air floatation suspension layer filtering device | |
| CN114477494B (en) | Phenol-ammonia wastewater treatment device and process for degassing and light-heavy oil separation treatment | |
| CN115925204A (en) | Offshore oilfield production water on-site treatment and on-site reinjection system and process | |
| CN206089115U (en) | Oil -water separation tower | |
| CN114538639B (en) | Pretreatment system and method for oily sewage before biochemical treatment | |
| CN210367068U (en) | Fracturing flow-back fluid and oil field produced water solid-liquid separation system | |
| CN212151802U (en) | Pretreatment equipment for grinding oil stains and SS in wastewater | |
| CN108529710B (en) | Strong whirl deoiling equipment of air supporting coalescence | |
| CN205687674U (en) | A kind of novel all-in-one oily water separating equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200421 |