CN111378487B - Device and method for removing suspended matters in oil products - Google Patents
Device and method for removing suspended matters in oil products Download PDFInfo
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- CN111378487B CN111378487B CN201811622911.2A CN201811622911A CN111378487B CN 111378487 B CN111378487 B CN 111378487B CN 201811622911 A CN201811622911 A CN 201811622911A CN 111378487 B CN111378487 B CN 111378487B
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
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Abstract
A device and method for removing suspended matters in oil products, the device comprises at least two stages of air-flotation removing sections which are sequentially arranged from bottom to top, the porosity of filler in the upper air-flotation removing section is always smaller than that of filler in the lower air-flotation removing section, a micro-bubble generator is arranged at the bottom of the first-stage air-flotation removing section, and high-air-volume and low-air-volume pulse type air inlet is adopted to uniformly arrange suspended matters attached to the surfaces of the fillers and dredge the pores among the fillers; the invention adopts the low-density type filler, the filler is in a non-fixed state in the air floatation removal section, and the pulse type ventilation makes the filler do self-rotation motion or collision motion, so that suspended matters are uniformly attached to the surface of the air floatation filler, not only the suspended matters in the raw materials are effectively removed, but also the filler is prevented from being blocked by the suspended matters.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a device for removing suspended matters in oil products and a method for removing the suspended matters by using the device.
Background
The crude oil contains water and salts such as sodium chloride, calcium chloride, magnesium chloride and the like, in order to not influence the processing of the crude oil, the crude oil is desalted and dehydrated in the first step before entering a factory for processing, so that the water content is 0.1-0.2 percent, and the salt content is less than 5mg/L, but the requirements of the refinery with residual oil hydrogenation or heavy oil cracking are stricter, the salt content in the crude oil is less than 3mg/L, and along with the enhancement of the trend of crude oil deterioration and heaviness, more crude oil contains a certain amount of colloid suspended matters, so that more problems are brought to the dehydration and desalination process of the crude oil and subsequent processing devices, and the main performance is as follows: (1) colloidal suspended matters in the crude oil are suspended in oil products in a flaky manner, so that the flowing equipment and pipelines are easily blocked; (2) the colloid suspended matters are not easy to be polarized in the traditional electric desalting process, so that the oil-water separation is difficult to realize, the oil-water separation is incomplete, and the two phases are seriously carried with each other; (3) the removal of these colloidal suspensions is highly likely to cause filter clogging using conventional filtration methods. In short, because of the existence of colloidal suspended matters, after the raw oil is subjected to electric desalting by the traditional method, the colloidal suspended matters are very unfavorable in oil products and sewage, and need to be removed and then subjected to oil-water separation.
In the prior art, crude oil pretreatment adopts an electric desalting and dewatering method, and a process and equipment for removing colloid suspended matters are not arranged, so that the method has the following problems: (1) colloid suspended matters cannot be removed in the electric desalting process, cannot be settled and separated, cannot be polarized by an electric field, influence the desalting effect, and are the main reasons for the unqualified salt content index in the desalted crude oil; (2) the colloid suspended substance is an oil substance with light density but is insoluble in water, so that the oil-water separation effect is influenced in the oil-water separation process, the oil-water two phases are very seriously carried with each other, and the water content in the oil product is higher. Therefore, if the oil product is desalted or dehydrated with good effect, new process and equipment need to be developed to remove suspended matters from the oil product, so as to solve the problems of poor desalting effect, serious mutual entrainment of oil and water phases and the like in the desalting and dehydrating process of the oil product.
CN201280072453.4 proposes a filter device and a method for filtering suspensions, wherein the filter device has a pack of at least one recess plate and adjacent recess plates, said pack being between a fixed head piece and a movable end piece, the filter device having a suspension pipe for piping a first flow of suspension from the head piece into the pack, said suspension pipe extending through said pack to the end piece, wherein the filter device has a supply pipe for conveying a second flow pipe of the suspension into the suspension pipe, said connection supply pipe being connected to the end piece, wherein a filter cavity is formed between the recess plate and the adjacent recess plate, the recess plate and/or the adjacent recess plate having a recess, wherein the recess plate has a suspension conduit for conveying the suspension from the suspension pipe to the filter chamber, the filter device having at least one filter cloth for filtering solid components from the suspension. The principle of the method is that the suspended matters are filtered by adopting the principle of the filter cloth, and the problems that the filter cloth is easy to block and cannot be used for a long time still exist.
CN201810070840.3 proposes a method and a system for zero discharge of salt-containing wastewater, wherein the method comprises the steps of further removing hardness and silicon from colloid removed from suspended matters by a lime-soda softening method and dissolved air flotation filtration; removing hardness by ion exchange depth; adopts advanced oxidation and high-salt microbial biological combined technology to further reduce COD and NO by adopting RO concentrated water advanced treatment3And NF membrane salt separation process; concentrating and separating salt by adopting a constant-temperature evaporative crystallization process through a multi-effect MVR, wherein concentrated water discharged by the MVR is introduced into a catalytic oxidation membrane or an NF membrane or is completely introduced into mixed salt MVR to produce mixed salt; mother liquor of the MVR device is discharged and enters a low-temperature freezing method to produce mirabilite in an increasing way to eliminate COD interference, and the freezing liquid is subjected to advanced oxidation to eliminate COD of the mother liquor discharged from the crystallization device. In the method, the traditional dissolved air flotation filtration mode is still adopted in the suspended matter removal process, and the mode has the problems of poor suspended matter removal effect, easy blockage of filtration equipment, incapability of long-term operation and the like.
In conclusion, the development of the method for removing suspended matters has great significance for solving the problems of poor desalting effect, blockage of filtering equipment, serious mutual entrainment of oil and water phases and the like in the oil product desalting and dewatering process.
Disclosure of Invention
Aiming at the problems that equipment capable of effectively removing suspended matters in oil products is lacked in the prior art, a device is easy to block in the removing process, the removing is not thorough, and the subsequent desalting effect is greatly influenced, the invention provides the device and the method for removing the suspended matters in the oil products, and the device and the method have good suspended matter removing effect and high treatment efficiency.
The technical purpose of the invention is realized by the following technical means:
the technical purpose of the first aspect of the invention is to provide a device for removing suspended matters in oil products, which comprises at least two stages of air flotation removal sections which are sequentially arranged from bottom to top, wherein the lowest layer is a first stage air flotation removal section, air flotation fillers are filled in the air flotation removal sections, and the porosity of the fillers in the air flotation removal section on the upper layer is always smaller than that of the fillers in the air flotation removal section on the lower layer; a micro-bubble generator is arranged at the bottom of the primary air floatation removal section, a valve capable of controlling air flow or a plurality of valves with different air flow are arranged at the inlet of the micro-bubble generator, and a pressurizing and air dissolving device and an air supplementing device are arranged on an inlet pipeline of the micro-bubble generator; the top of the air floatation removal section at the uppermost layer is connected with a gas-liquid separator, and the gas-liquid separator is connected with a pressurizing gas dissolving device; the bottom of one-level air supporting desorption section sets up the oil feed inlet of treating, and the air supporting desorption section top of the superiors sets up discharge gate I and discharge gate II of oil, the oil after I ejection of compact of discharge gate is handled, and the oil feed inlet of treating of one-level air supporting desorption section bottom is connected to discharge gate II.
In the above apparatus, it is further preferable that the packing in the air flotation removal section is a low-density type packing having a density of 50kg/m3～900kg/m3Preferably 300kg/m3～600kg/m3The filler of (3). The filler is in a non-fixed state in the air floatation removal section. The filler is made of oleophylic material or modified oleophylic material, and is selected from at least one of polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic acid and nylon, or is selected from material with oleophylic treatment on the surface. The packing may be any shape such as any one type of large-pore honeycomb packing, large-pore wire mesh packing, hollow packing, fabric packing, and corrugated corner packing.
In the device, as further optimization, the porosity of the filler in the first-stage air floatation removal section is 50-95%, preferably 60-80%; the porosity of the filler in the air floatation removal section at the uppermost layer is 10-50%, preferably 20-40%.
In the above device, as a further preferred, the pressurized air dissolving device is one or a combination of a dissolved air pump, a high-pressure jet pump and a pipeline dissolved air pump.
In the above apparatus, it is further preferable that the microbubble generator is an apparatus capable of dispersing gas into small-sized bubbles, or may be called as a micro bubble generator, a membrane tube micro-disperser, an ultra-micro bubble generator, or the like, and is capable of forming bubbles having a size of 50nm to 1000 μm, preferably 5 μm to 100 μm, and any apparatus capable of realizing the above functions can be used in the present invention.
In the above apparatus, it is further preferable that the air flotation removal section is provided at 2 to 4 stages.
The technical purpose of the second aspect of the invention is to provide a method for removing suspended matters from oil products by using the device, after the oil products to be treated are injected with water, the oil products enter the device from a feed inlet at the bottom of a first-stage air floatation removal section and are mixed with bubbles generated by a micro-bubble generator, the suspended matters float upwards along with the bubbles, the filler in the first-stage air floatation removal section has larger porosity, larger blocks of suspended matters are adhered to the filler, the oil products to be treated continuously move upwards and sequentially enter an upper air floatation removal section, the porosity of the filler is smaller and smaller, and the suspended matters are removed step by step; the microbubble generator adopts high tolerance and low tolerance pulsed to admit air, and low tolerance is admitted air and is made the filler of air supporting desorption section do autogyration motion and not collide mutually by control air input, and when low tolerance was admitted air, discharge gate I opened, and discharge gate II was closed, and high tolerance was admitted air and is control the air input and make and collide between the filler in the air supporting desorption section, and when high tolerance was admitted air, discharge gate I closed, and discharge gate II opened.
As will be appreciated by those skilled in the art, the suspended substances in crude oil are mostly lighter lipophilic substances, and the method of the present invention utilizes the gas flotation to remove suspended substances, mainly based on the dissolution characteristics of the gas in the liquid phase, and after mixing with the oil to be treated, the gas tiny bubbles are dispersed in the liquid, and the bubbles adhere to the suspended substances and are adsorbed and attached by the filler of the gas flotation removal section for removal. In general, the smaller porosity is beneficial to adhering and hanging more suspended matters, but the blockage and the pressure drop are easy to increase, and the larger porosity causes the penetration of the smaller suspended matters, so the removal is not thorough. The stage number of the arranged air floatation removal section is adjusted according to the property of the oil product to be treated and the removal effect requirement.
In the technical scheme of the invention, the microbubble generator adopts high-air-volume and low-air-volume pulse type air inlet, and when the low-air-volume air inlet is carried out, the filler does self-rotation motion, so that suspended matters can be more uniformly attached to the surface of the microbubble generator, and the suspended matters are removed; and when high-air-volume air inlet is carried out, collision occurs between the fillers, suspended matters attached to the surfaces of the fillers are uniformly distributed, and pores among the fillers are dredged, so that the long-period operation of the device is ensured.
In the method, at the top of the air floatation removal section at the uppermost layer, air floatation gas carries a small amount of oil products and is separated by a gas-liquid separator, the gas returns to a supercharging device and enters a micro-bubble generator for recycling, and insufficient gas is supplemented by a gas supplementing device.
In the method, as further optimization, the water injection amount to the oil product to be treated is 3-20% of the mass of the crude oil.
In the above process, as a further preference, the gas used in the gas flotation removal section is selected from nitrogen, air or an inert gas, preferably nitrogen.
In the above method, the ratio of the low-volume aeration time to the high-volume aeration time is more preferably 2:1 to 200:1, and most preferably 20:1 to 100: 1. In a more specific embodiment, the low-air-flow time is 60 to 1500 minutes, preferably 100 to 900 minutes, and the high-air-flow time is 0.5 to 100 minutes, preferably 5 to 30 minutes. More specifically, in low-gas aeration, the volume ratio of aeration to crude oil to be treated (Nm)3/h：m3The volume ratio of ventilation volume to crude oil to be treated (Nm) during high-air ventilation is 100: 1-600: 13/h：m3H) is 500:1 to 1000: 1; wherein the gas volume is based on the gas volume in the standard state.
In the above method, the size of the bubbles formed by the microbubble generator is more preferably 50nm to 1000 μm, and still more preferably 5 μm to 100 μm.
In the above method, as a further preferable mode, the operating conditions of the air flotation removal section are as follows: the temperature is normal temperature to 180 ℃, preferably 60 to 150 ℃; the pressure is 0.3 to 10.0MPa, preferably 0.5 to 2.0 MPa.
In the above method, as a further preference, the retention time of the oil to be treated in each stage of the air flotation removal section is 0.5 to 30 minutes, preferably 3 to 10 minutes.
In the method, the oil to be treated is selected from any one of heavy inferior raw oil, heavy dirty oil and coal tar, or is the oil product after the electric desalting of the raw oil or the cut oily sewage.
Compared with the prior art, the invention has the following advantages:
the device and the method adopt the low-density type filler, the filler is in an unfixed state in the air floatation removal section, pulse type ventilation enables the filler to do self-rotation motion or collision motion, and suspended matters are uniformly attached to the surface of the air floatation filler during low-air ventilation, so that the suspended matters in the raw materials are effectively removed; when the high-air-volume ventilation is carried out, suspended solids are not only uniformly attached to the surface of the air flotation filler, but also loose large suspended solids can be dropped through the collision of the filler, so that the homogenization effect is achieved, and the filler is prevented from being blocked by the suspended solids.
Drawings
FIG. 1 shows an apparatus for removing suspended matters from an oil product in example 1.
The device comprises a micro-bubble generator 1, a primary air-flotation removal section 2, a primary air-flotation packing layer 3, a secondary air-flotation removal section 4, a secondary air-flotation packing layer 5, a gas-liquid separator 6, an air supply device 7, a high-pressure dissolved air pump 8, a low-air-volume air inlet valve 9, a high-air-volume air inlet valve 10, a feed inlet 11, a discharge outlet I12, a discharge outlet II 13 and a discharge outlet I12.
Detailed Description
The invention is described in detail below with reference to the figures and examples, but the invention is not limited thereby.
Example 1
A device for removing suspended substances in oil products, as shown in figure 1, comprises a first-stage air-flotation removal section 2 and a second-stage air-flotation removal section 4 which are sequentially arranged from bottom to top, wherein the first-stage air-flotation removal section 2 is filled with a first-stage air-flotation filler layer 3, the filler is macroporous honeycomb filler, and the density is 550kg/m3The porosity is 65% -70%; the second-stage air-flotation removal section 4 is filled with a second-stage air-flotation filler layer 5 which is macroporous honeycomb filler with the density of 570kg/m3The porosity is 25% -30%; the fillers are all polypropylene fillers; the bottom of the first-stage air flotation removal section 2The device is provided with a micro-bubble generator 1, the inlet of the micro-bubble generator 1 is provided with a low-air inlet valve 9 and a high-air inlet valve 10 which can control air flow, and the inlet pipeline of the micro-bubble generator 1 is provided with a high-pressure dissolved air pump 8 and an air supplementing device 7; the top of the secondary air floatation removal section 5 is connected with a gas-liquid separator 6, and the gas-liquid separator 6 is connected with a high-pressure dissolved air pump 8; the bottom of the first-stage air-flotation removal section is provided with a feed inlet 11 for oil products to be treated, and the top of the second-stage air-flotation removal section 5 is provided with a discharge outlet I12 and a discharge outlet II 13 for the treated oil products.
Example 2
Except that the first-stage air-flotation packing layer 3 is filled with macroporous wire mesh packing, the porosity is 70-75%, and the second-stage air-flotation packing layer 5 is filled with 20-25%, the device for removing suspended matters in oil products has the same structure and arrangement mode as those of the device in the embodiment 1.
Example 3
Except that the first-stage air-flotation packing layer 3 is filled with macroporous silk screen packing, the porosity is 65-70%, and the second-stage air-flotation packing layer 5 is filled with 20-25%, the device for removing suspended matters in oil products has the same structure and arrangement mode as those of the device in the embodiment 1.
Example 4
The feedstock oil from a certain plant was treated for removal of suspended matter using the apparatus of example 1, and the properties of the feedstock oil are shown in table 1, and the feedstock oil is a heavy dirty oil and is characterized by high density, high viscosity, and a large amount of suspended matter.
TABLE 1
Injecting 12wt% of raw oil water into the device from a bottom feed inlet 11 of the primary air-flotation removal section 2, mixing the raw oil water with bubbles generated by the micro-bubble generator 1, wherein suspended matters float upwards along with the bubbles, larger suspended matters are adhered by the filler of the primary air-flotation filler layer 3, the raw oil continuously flows upwards to enter the secondary air-flotation removal section 4, and the rest small suspended matters are adhered by the filler of the secondary air-flotation filler layer 5; the microbubble generator 1 adopts high-air-volume and low-air-volume pulse type air intake, the single low-air-volume air intake time is 720 minutes, and the air intake is cutChanging to high-air ventilation, wherein the single high-air ventilation time is 18 minutes, and the ratio of the low-air ventilation time to the high-air ventilation time is 40: 1; when air is fed at low air flow, the air inlet flow is controlled to make the filler in the air-float removing section do self-rotating motion without mutual collision, and the volume ratio (Nm) of air flow and raw oil3/h：m3The ratio of the pressure to the pressure is 600:1, the discharge port I12 is opened, and the discharge port II 13 is closed; when high-air-volume air inflow is carried out, the air inflow is controlled to lead the fillers in the air floatation removal section to collide with each other, and the volume ratio (Nm) of the air flow to the raw oil3/h：m3The ratio of the pressure to the pressure is 900:1, the discharge port I12 is closed, and the discharge port II 13 is opened.
The operating temperature in the first-stage air flotation removal section 2 and the second-stage air flotation removal section 4 is 125-135 ℃, and the operating pressure is 0.8-1.0 MPaG; the total retention time of the crude oil is 30 minutes, wherein the retention time in the first-stage air flotation removal section 2 is 15 minutes, and the retention time in the second-stage air flotation removal section 4 is 15 minutes.
The above crude oil treatment process adopts nitrogen gas as gas floating gas, the microbubble generator adopts a microporous plate, and the size of microbubbles formed by the controller through the microporous plate is 500 μm.
The treated crude oil collected from the discharge port I12 is subjected to standing sedimentation for 24 hours, the obtained upper layer is an oil phase, the obtained lower layer is a water phase, the oil-water separation interface is clear, the water content in the analyzed oil phase is 1.45-1.72%, the oil content in the water phase is 0.78-0.89%, and suspended matters are completely removed.
Example 5
The crude oil from the same source as above was processed using the apparatus of example 2, the procedure was the same as in example 4.
The specific operating conditions were as follows:
the water injection amount is 10 percent of the mass of the raw materials;
the single low-air ventilation time is 360 minutes, the high-air ventilation is switched, the single high-air ventilation time is 6 minutes, and the ratio of the low-air ventilation time to the high-air ventilation time is 60: 1; volume ratio (Nm) of ventilation to feedstock oil at low air intake3/h：m3H) 400: 1; volume ratio (Nm) of ventilation to feedstock oil at high air intake3/h：m3The/h) is 700: 1.
The operating temperature in the first-stage air floatation removal section 2 and the second-stage air floatation removal section 4 is 90-110 ℃, and the operating pressure is 0.8-1.0 MPaG; the total residence time of the crude oil was 45 minutes, with the residence time in the first-stage air-flotation removal section 2 being 25 minutes and the residence time in the second-stage air-flotation removal section 4 being 20 minutes.
The above crude oil treatment process adopts nitrogen gas as gas floating gas, the microbubble generator adopts a microporous plate, and the size of microbubbles formed by the controller through the microporous plate is 100 μm.
The treated crude oil collected from the discharge port I12 is subjected to standing sedimentation for 24 hours, the obtained upper layer is an oil phase, the obtained lower layer is a water phase, the oil-water separation interface is clear, the water content in the analyzed oil phase is 1.38-1.52%, the oil content in the water phase is 0.66-0.85%, and suspended matters are completely removed.
Example 6
The crude oil from the same source as above was processed using the apparatus of example 3, the procedure was the same as in example 4.
The specific operating conditions were as follows:
the water injection amount is 15 percent of the mass of the raw materials;
the single low-air ventilation time is 900 minutes, the high-air ventilation is switched, the single high-air ventilation time is 25 minutes, and the ratio of the low-air ventilation time to the high-air ventilation time is 36: 1; volume ratio (Nm) of ventilation to feedstock oil at low air intake3/h：m3H) 500: 1; volume ratio (Nm) of ventilation to feedstock oil at high air intake3/h：m3The/h) is 800: 1.
The operating temperature in the first-stage air flotation removal section 2 and the second-stage air flotation removal section 4 is 75-95 ℃, and the operating pressure is 0.8-1.0 MPaG; the total retention time of the crude oil is 40 minutes, wherein the retention time in the first-stage air flotation removal section 2 is 20 minutes, and the retention time in the second-stage air flotation removal section 4 is 20 minutes.
The above crude oil treatment process adopts nitrogen gas as gas floating gas, the microbubble generator adopts a microporous plate, and the size of microbubbles formed by the controller through the microporous plate is 50 μm.
The treated crude oil collected from the discharge port I12 is subjected to standing sedimentation for 24 hours, the obtained upper layer is an oil phase, the obtained lower layer is a water phase, the oil-water separation interface is clear, the water content in the analyzed oil phase is 1.40-1.58%, the oil content in the water phase is 0.71-0.83%, and suspended matters are completely removed.
Comparative example 1
The crude oil of table 1 was deflocculated using conventional air flotation.
The air floatation process adopts conventional air floatation filtration equipment, which comprises a dissolved air tank, an aeration head, a gas compressor unit, a floatation tank, a filter and related accessories, wherein the air floatation is air.
The raw materials and the water injection are mixed and then firstly enter a dissolved air tank, the air flotation air also enters the dissolved air tank after being boosted by a compressor, the high-pressure dissolved air of the raw materials is completed in the dissolved air tank, the feed dissolved with a large amount of gas enters a flotation tank, the air flotation is carried out after the aeration of an aeration head at the bottom of the flotation tank, the suspended matters are carried to the upper part of the flotation tank by utilizing air bubbles, then the materials at the upper part of the flotation tank are introduced into a filter again, and the suspended matters are removed in a filtering mode.
The operating conditions were as follows: operating temperature: 128-140 ℃; operating pressure: 0.8-1.0 MPaG; total residence time: 40 minutes; the supplementary water injection amount is 15 percent of the mass of the raw materials.
In the process of removing suspended matters from raw materials, the obtained feed liquid without the suspended matters is subjected to standing sedimentation for 24 hours, the obtained upper layer is an oil phase, the obtained lower layer is a water phase, but an oil-water separation interface is unclear, and meanwhile, the filter is blocked in about 12 minutes in the process of removing the suspended matters, so that the suspended matter removing process cannot be operated for a long time; the water content in the oil phase was analyzed to be 11.2%, the oil content in the water phase was 5.64%, and the water phase contained a large amount of dark-black suspended matter.
The experiments show that compared with the traditional air flotation filtration method, the device and the method have the advantages of ideal effect of removing suspended matters and capability of ensuring long-period operation, particularly for heavy/poor oil products with high density, high viscosity and high content of suspended matters, the suspended matters are difficult to remove, and the suspended matters have great influence on the oil-water separation effect, so that the problems of large amount of water carrying of oil and water, high oil content in water, incapability of separating oil and water and the like can be caused if the effect of removing the suspended matters is not ideal.
Claims (19)
1. The device for removing suspended matters in oil products is characterized by comprising at least two stages of air flotation removal sections which are sequentially arranged from bottom to top, wherein the lowest layer is a first-stage air flotation removal section, air flotation fillers are filled in the air flotation removal sections, and the fillers are low-density fillers with the density of 50kg/m3～900kg/m3The air flotation removing section is in an unfixed state, the porosity of the filler in the first-stage air flotation removing section is 50-95%, the porosity of the filler in the uppermost air flotation removing section is 10-50%, and the porosity of the filler in the upper air flotation removing section is always smaller than the porosity of the filler in the lower air flotation removing section; the bottom of the first-stage air floatation removal section is provided with a micro-bubble generator, the micro-bubble generator is equipment capable of forming bubbles with the size of 50 nm-1000 mu m, high-air-volume and low-air-volume pulse type air inlet is adopted, an inlet of the micro-bubble generator is provided with a valve capable of controlling air volume or a plurality of valves with different air volumes, and an inlet pipeline of the micro-bubble generator is provided with a pressurizing air dissolving device and an air supplementing device; the top of the air floatation removal section at the uppermost layer is connected with a gas-liquid separator, and the gas-liquid separator is connected with a pressurizing gas dissolving device; the bottom of one-level air supporting desorption section sets up the oil feed inlet of treating, and the air supporting desorption section top of the superiors sets up discharge gate I and discharge gate II of oil, the oil after I ejection of compact of discharge gate is handled, and the oil feed inlet of treating of one-level air supporting desorption section bottom is connected to discharge gate II.
2. The device of claim 1, wherein the filler is made of oleophilic material or modified oleophilic material selected from at least one of polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic and nylon, or from oleophilic treated material of the material surface.
3. The device of claim 1, wherein the pressurized air dissolving device is one or more of a combination of an air dissolving pump, a high-pressure jet pump and a pipeline air dissolving pump.
4. The device as claimed in claim 1, wherein the air floatation removal section is provided with 2-4 stages.
5. The method for removing suspended matters from oil products by using the device of any one of claims 1 to 4, after the oil products to be treated are injected with water, the injected oil products enter the device from a feed inlet at the bottom of a first-stage air floatation removal section and are mixed with bubbles generated by a micro-bubble generator, the suspended matters float upwards along with the bubbles, the filler in the first-stage air floatation removal section has larger porosity, larger blocks of suspended matters are adhered to the filler, the oil products to be treated continuously move upwards and sequentially enter an upper air floatation removal section, the porosity of the filler is smaller and smaller, and the suspended matters are removed step by step; the microbubble generator adopts high tolerance and low tolerance pulsed to admit air, and low tolerance is admitted air and is made the filler of air supporting desorption section do autogyration motion and not collide mutually by control air input, and when low tolerance was admitted air, discharge gate I opened, and discharge gate II was closed, and high tolerance was admitted air and is control the air input and make and collide between the filler in the air supporting desorption section, and when high tolerance was admitted air, discharge gate I closed, and discharge gate II opened.
6. The method as claimed in claim 5, wherein at the top of the uppermost flotation removal section, the flotation gas carrying a small amount of oil is separated by a gas-liquid separator, the gas is returned to a pressurizing device and enters the microbubble generator for recycling, and the insufficient gas is supplemented by a gas supplementing device.
7. The method of claim 5, wherein the water is injected into the oil to be treated in an amount of 3% to 20% by mass of the crude oil.
8. The process of claim 5, wherein the gas used in the gas flotation removal section is selected from nitrogen, air or an inert gas.
9. The method of claim 8, wherein the gas used in the gas flotation removal section is nitrogen.
10. The method of claim 5, wherein the ratio of low-volume aeration time to high-volume aeration time is from 2:1 to 200: 1.
11. The method according to claim 5, wherein the ratio of the low-volume aeration time to the high-volume aeration time is 20:1 to 100: 1.
12. The method of claim 5, wherein the time interval between switching the low-volume ventilation and the high-volume ventilation is 60-1500 minutes.
13. The method according to claim 5, wherein the volume ratio of the ventilation volume to the crude oil to be treated is 100: 1-600: 1 during low-gas ventilation.
14. The method according to claim 5, wherein the volume ratio of the ventilation volume to the crude oil to be treated is 500: 1-1000: 1 during the high-air ventilation.
15. The method of claim 5, wherein the microbubble generator forms bubbles having a size of 50nm to 1000 μm.
16. The method of claim 15, wherein the microbubble generator forms bubbles having a size of 5 μm to 100 μm.
17. The process of claim 5, wherein the operating conditions of the air flotation removal section are as follows: the temperature is normal temperature to 180 ℃, and the pressure is 0.3 to 10.0 MPa.
18. The process of claim 17, wherein the operating conditions of the air flotation removal section are as follows: the temperature is 60-150 ℃, and the pressure is 0.5-2.0 MPa.
19. The method as claimed in claim 5, wherein the retention time of the oil to be treated in each stage of the air flotation removal section is 0.5-30 minutes.
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| CN104355476A (en) * | 2014-11-25 | 2015-02-18 | 成都国盛环境保护技术有限公司 | Process and device for overall standard-reached treatment for oil-gas field drilling waste |
| CN105698841A (en) * | 2016-03-27 | 2016-06-22 | 中国石油大学(华东) | Oil-containing sewage cyclone flotation evaluation device and method using same |
| CN106277150A (en) * | 2016-09-07 | 2017-01-04 | 珠海巨涛海洋石油服务有限公司 | Microbubble aerator and using method thereof are selected in a kind of oil-water process air supporting |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104355476A (en) * | 2014-11-25 | 2015-02-18 | 成都国盛环境保护技术有限公司 | Process and device for overall standard-reached treatment for oil-gas field drilling waste |
| CN105698841A (en) * | 2016-03-27 | 2016-06-22 | 中国石油大学(华东) | Oil-containing sewage cyclone flotation evaluation device and method using same |
| CN106277150A (en) * | 2016-09-07 | 2017-01-04 | 珠海巨涛海洋石油服务有限公司 | Microbubble aerator and using method thereof are selected in a kind of oil-water process air supporting |
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