CN111378486B - Device and method for continuously removing suspended matters in crude oil - Google Patents
Device and method for continuously removing suspended matters in crude oil Download PDFInfo
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- CN111378486B CN111378486B CN201811622905.7A CN201811622905A CN111378486B CN 111378486 B CN111378486 B CN 111378486B CN 201811622905 A CN201811622905 A CN 201811622905A CN 111378486 B CN111378486 B CN 111378486B
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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
The device comprises two sets of air flotation removal systems, each set of air flotation removal system comprises at least two stages of air flotation removal sections which are sequentially arranged from bottom to top, the porosity of the filler in the upper air flotation removal section is always smaller than that of the filler in the lower air flotation removal section, a micro bubble generator is arranged at the bottom of the first air flotation removal section, and low-air-volume air intake is adopted when the suspended matters in the crude oil are removed, and high-air-volume air intake is adopted when the suspended matters in the filler are desorbed. According to the invention, while suspended matters in raw materials are effectively removed, the cleaning and purification of the filler and the desorption of the suspended matters are realized on line, the problems that the adsorption efficiency is reduced and even the filler is blocked by the suspended matters due to the increase of the suspended matters on the surface of the filler can be prevented, and the long-period and high-efficiency operation of the device is ensured.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a device for continuously removing suspended matters in crude oil 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 device and the method for continuously removing the suspended matters in the crude oil are developed, and the device and the method have important 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
The invention provides a device and a method for continuously removing suspended matters in crude oil, which have good suspended matter removing effect and high treatment efficiency and aim to solve the problems that equipment capable of effectively removing the suspended matters in the crude oil is lacked, a device is easy to block in the removing process, the removing is not thorough, and the subsequent desalting effect is greatly influenced in the prior art.
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 continuously removing suspended matters in crude oil, which comprises two sets of air floatation removal systems, wherein each set of air floatation removal system comprises at least two stages of air floatation removal sections which are sequentially arranged from bottom to top, the lowest layer is a first stage air floatation removal section, air floatation fillers are filled in the air floatation removal sections, and the porosity of the fillers in the air floatation removal section at the upper layer is always smaller than that of the fillers in the air floatation removal section at 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 provided with a gas outlet which is connected with a gas-liquid separator, and the gas-liquid separator is connected with a pressurizing gas dissolving device; the bottom of the first-stage air floatation removal section is provided with a feed inlet, and the top of the uppermost air floatation removal section is provided with a discharge outlet.
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, the air flotation removal section is preferably provided at 2 to 4 stages, and more preferably at 2 stages.
The technical purpose of the second aspect of the invention is to provide a method for continuously removing suspended matters from crude oil by using the device, after the crude oil to be treated is injected with water, the crude oil enters the device from a feed inlet at the bottom of a first-stage air floatation removal section of one set of air floatation removal system and is 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 crude oil to be treated continuously moves upwards and sequentially enters an upper air floatation removal section, the porosity of the filler is smaller and smaller, the suspended matters are removed step by step, and the treated crude oil is collected from a discharge outlet at the top of the uppermost air floatation removal section; the microbubble generator adopts low-air-volume air inlet, and the low-air-volume air inlet controls air inlet quantity to enable the filler in the air floatation removing section to make self-rotation motion without mutual collision; when filler absorption suspended solid in this air supporting desorption system is saturated, switch crude oil and carry out the suspended solid desorption by another set of air supporting desorption system feeding, and carry out the suspended solid desorption process in the filler with this set of air supporting desorption system, switch into carrying oil with the feeding, microbubble generator adopts high-capacity air admission simultaneously, high-capacity air admission is that control air input makes and takes place collision each other between the filler in the air supporting desorption section, make its absorbent suspended solid drop, is taken away by carrying oil, is collected by the discharge gate.
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 property of the gas in the liquid phase, and after mixing with the crude 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, in the process of removing suspended matters from crude oil, the microbubble generator adopts low-gas-flow gas inlet, and the filler performs self-rotation motion, so that the suspended matters can be more uniformly attached to the surface of the microbubble generator, and the removal of the suspended matters is completed; in the process of carrying out suspended matter elution by virtue of filler adsorption saturation, the microbubble generator adopts high-air-volume air inlet, the suspended matters attached to the surface of the filler are removed by virtue of collision between the fillers, the suspended matters are taken out of the system along with carrying oil added by the system, elution is completed, and the long-period operation of the device is ensured.
In the method, a gas-liquid separator is arranged at the top of the air floatation removal section at the uppermost layer for gas-liquid separation, the separated 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, the carrying oil is various types of oil products or organic solvents which do not contain suspended matters, have low viscosity and good properties, and is selected from at least one of organic solvents of gasoline, kerosene, diesel oil, benzenes, esters, acids, ketones and aldehydes. The carrying oil is continuously or intermittently introduced.
In the method, as a further preference, the water is injected into the crude oil to be treated in an amount of 3-20% by mass of the crude oil.
In the above method, as further preferred, the gas introduced into the system is selected from nitrogen, air or an inert gas, preferably nitrogen.
In the above method, as a further preferred aspect, the volume ratio (Nm) of the ventilation to the crude oil to be treated at the time of aeration at a low gas level3/h：m3The volume ratio of ventilation volume to carrying oil (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 residence time of the crude oil or carrying oil to be treated in each stage of the air flotation removal section is 0.5 to 500 minutes, preferably 3 to 300 minutes.
In the method, the crude oil to be treated is selected from any one of heavy inferior raw oil, heavy dirty oil and coal tar, or is an oil product obtained after crude oil is electrically desalted or cut oily sewage.
Compared with the prior art, the invention has the following advantages:
(1) the device and the method adopt the low-density filler which is in a non-fixed state in the air floatation removal section and can continuously move in the process of removing suspended matters, so that the filler is uniformly attached with the suspended matters to play a role of homogenization on one hand, and the air floatation filler is prevented from being blocked by the suspended matters and even being blocked on the other hand;
(2) when suspended matters in the crude oil are removed, low-air-volume air inlet is adopted, so that the filler performs self-rotation motion, the suspended matters are uniformly attached to the surface of the filler, and the suspended matters in the crude oil can be effectively removed; when the suspended solid in the filler is desorbed when needs are carried out, the high-air-volume air inlet is adopted, so that the fillers are mutually collided, the adsorbed suspended solid in the filler is desorbed and is carried away by the carried oil introduced into the system, the filler is prevented from being blocked by the suspended solid, the suspended solid desorption of crude oil and the suspended solid desorption of the filler are alternately carried out, and the continuous suspended solid desorption of the crude oil is realized.
In a word, the invention can effectively remove suspended matters in raw materials and simultaneously realize the cleaning and purification of the filler on line, can prevent the problem that the adsorption efficiency is reduced and even the filler is blocked by the suspended matters along with the increase of the suspended matters on the surface of the filler, and ensures the long-period operation of the device.
Drawings
FIG. 1 is a schematic diagram of the apparatus for continuously removing suspended substances from crude oil in example 1.
The air flotation device comprises a 100-degree air flotation removal system I, a 200-degree air flotation removal system II, a 1A-degree micro-bubble generator, a 2A-degree air flotation removal section, a 3A-degree air flotation packing layer, a 4A-degree secondary air flotation removal section, a 5A-degree secondary air flotation packing layer, a 6A-degree gas-liquid separator, a 7A-degree air supply device, a 8A-degree high-pressure dissolved air pump, a 9A-degree feed inlet, a 10A-degree discharge outlet, a 1B-degree micro-bubble generator, a 2B-degree air flotation removal section, a 3B-degree primary air flotation packing layer, a 4B-degree secondary air flotation removal section, a 5B-degree secondary air flotation packing layer, a 6B-degree gas-liquid separator, a 7B-degree air supply device, a 8B.
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 continuously removing suspended matters in crude oil comprises an air floatation removal system I100 and an air floatation removal system II 200, wherein the air floatation removal system I100 comprises a first-stage air floatation removal section 2A and a second-stage air floatation removal section 4A which are sequentially arranged from bottom to top, a first-stage air floatation filler layer 3A is filled in the first-stage air floatation removal section 2A, the filler is macroporous honeycomb filler, and the density is 550kg/m3The porosity is 65% -70%; the second-stage air-flotation removal section 4A is filled with a second-stage air-flotation filler layer 5A, the filler is macroporous honeycomb filler, and the density is 570kg/m3The porosity is 25% -30%; the fillers are all polypropylene fillers; a micro-bubble generator 1A is arranged at the bottom of the primary air floatation removal section 2A, an air inlet valve capable of controlling air flow is arranged at the inlet of the micro-bubble generator 1A, and a high-pressure dissolved air pump 8A and an air supply device 7A are arranged on an inlet pipeline of the micro-bubble generator 1A; the top of the secondary air floatation removal section 5A is connected with a gas-liquid separator 6A, and the gas-liquid separator 6A is connected with a high-pressure dissolved air pump 8A; the bottom of the first-stage air floatation removal section is provided with a feeding hole 9A for oil products to be treated, and the top of the second-stage air floatation removal section 5A is provided with a discharging hole 10A for treated crude oil or carrying oil;
the structure and the arrangement mode of the air floatation removing system II 200 are the same as those of the air floatation removing system I100, and the air floatation removing system II comprises a first-stage air floatation removing section 2B and a second-stage air floatation removing section 2B which are sequentially arranged from bottom to topA removing section 4B, a first-stage air-flotation filler layer 3B is filled in the first-stage air-flotation removing section 2B, the filler is macroporous honeycomb filler with the density of 550kg/m3The porosity is 65% -70%; the second-stage air-flotation removal section 4B is filled with a second-stage air-flotation filler layer 5B, the filler is macroporous honeycomb filler, and the density is 570kg/m3The porosity is 25% -30%; the fillers are all polypropylene fillers; a micro-bubble generator 1B is arranged at the bottom of the primary air floatation removal section 2B, an air inlet valve capable of controlling air flow is arranged at the inlet of the micro-bubble generator 1B, and a high-pressure dissolved air pump 8B and an air supply device 7B are arranged on an inlet pipeline of the micro-bubble generator 1A; the top of the secondary air floatation removal section 5B is connected with a gas-liquid separator 6B, and the gas-liquid separator 6B is connected with a high-pressure dissolved air pump 8B; the bottom of the first-stage air floatation removal section is provided with a feeding hole 9B for oil products to be treated, and the top of the second-stage air floatation removal section 5B is provided with a discharging hole 10B for treated crude oil or carrying oil;
the crude oil to be treated and the oil-carrying feed are connected to feed port 9A and feed port 9B.
Example 2
The device for continuously removing suspended matters in crude oil has the same structure and arrangement mode as those of the embodiment 1 except that the porosity of the first-stage air flotation packing layers 3A and 3B is 75-80%, and the porosity of the second-stage air flotation packing layers 5A and 5B is 30-35%.
Example 3
Except that the first-stage air- flotation packing layers 3A and 3B are filled with macroporous silk screen packing, the porosity is 65-70%, and the second-stage air- flotation packing layers 5A and 5B are filled with the macroporous silk screen packing, the device for removing suspended matters in oil products has the same structure and arrangement mode as those of 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
Mixing the above raw materialsAfter 12wt% of the raw oil is injected with water, the raw oil enters a device from a bottom feed inlet 9A of a primary air-flotation removal section 2A of an air-flotation removal system I100 and is mixed with bubbles generated by a micro-bubble generator 1A, suspended matters in the raw oil float upwards along with the bubbles, larger suspended matters are adhered by a filler of a primary air-flotation filler layer 3A, the raw oil continuously moves upwards to enter a secondary air-flotation removal section 4A, and the rest small suspended matters are adhered by a filler of a secondary air-flotation filler layer 5A; the microbubble generator 1A adopts low-air-volume air inlet, controls the air inlet volume to enable the filler in the air floatation removing section to do self-rotation motion without mutual collision, and has the volume ratio (Nm) of the air volume to the raw oil3/h：m3H) is 600:1, and the treated raw oil is collected from a discharge port 10A. The air flotation removal system I100 carries out the work of removing suspended matters from the raw oil, after the filler is adsorbed and saturated, the raw oil feeding is switched to the air flotation removal system II 200, the carrier oil is fed into the air flotation removal system I100 and is light diesel oil, the microbubble generator 1A is switched to high-air-volume air feeding at the same time, the air feeding amount is controlled to enable the filler in the air flotation removal section to collide, the suspended matters adsorbed by the filler fall off and are taken out of the system by the carrier oil, and the volume ratio (Nm) of the ventilation volume to the raw oil volume is3/h：m3H) 900:1, and collecting the carrying oil with suspended matters removed from the discharge hole 10A.
When the raw oil is subjected to suspended matter removal treatment, the operating temperature in the primary air flotation removal section 2A and the secondary air flotation removal section 4A is 120-130 ℃, and the operating pressure is 0.8-1.0 MPaG; the total retention time of the raw oil is 30 minutes, wherein the retention time in the first-stage air flotation removal section 2A is 15 minutes, and the retention time in the second-stage air flotation removal section 4A is 15 minutes.
When the suspended matters are desorbed by the filler, the operating temperature in the first-stage air-flotation removal section 2A and the second-stage air-flotation removal section 4A is 120-130 ℃, and the operating pressure is 0.4-0.5 MPaG; the total retention time of the carrying oil was 120 minutes, wherein the retention time in the first-stage air-flotation removal section 2A was 60 minutes, and the retention time in the second-stage air-flotation removal section 4A was 60 minutes.
The air-float gas in the above-mentioned processing procedure adopts nitrogen gas, and the microbubble generator adopts the micropore board, and the microbubble size that the controller formed through the micropore board is 500 μm.
The treated crude oil collected from the discharge port 10A 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 1.24-1.52%, the oil content in the water phase is 0.68-0.72%, suspended matters are completely removed, and the device runs stably for a long period.
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 8 percent of the mass of the raw materials;
volume ratio (Nm) of ventilation to stock oil at low gas inflow in stock oil suspension removal treatment3/h：m3H) 500: 1; the operating temperature in the first-stage air floatation removal section 2A and the second-stage air floatation removal section 4A is 100-110 ℃, and the operating pressure is 0.8-1.0 MPaG; the total retention time of the raw oil is 30 minutes, wherein the retention time in the first-stage air flotation removal section 2A is 15 minutes, and the retention time in the second-stage air flotation removal section 4A is 15 minutes.
Volume ratio (Nm) of ventilation to raw oil in high-air intake during desorption of suspended matter from filler3/h：m3The ratio of the first-stage air flotation removal section 2A to the second-stage air flotation removal section 4A to the second-stage air flotation removal section is 800:1, the operating temperature in the first-stage air flotation removal section 2A and the second-stage air flotation removal section 4A is 100-110 ℃, and the operating pressure is 0.4-0.5 MPaG; the total retention time of the carrying oil was 160 minutes, wherein the retention time in the first-stage air-flotation removal section 2A was 80 minutes, and the retention time in the second-stage air-flotation removal section 4A was 80 minutes.
The air-float gas in the above-mentioned processing procedure adopts nitrogen gas, and the microbubble generator adopts the micropore board, and the microbubble size that the controller formed through the micropore board is 100 μm.
The treated crude oil collected from the discharge port 10A 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 1.32-1.47%, the oil content in the water phase is 0.60-0.71%, all suspended matters are removed, and the device runs stably for a long period.
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;
volume ratio (Nm) of ventilation to stock oil at low gas inflow in stock oil suspension removal treatment3/h：m3H) 300: 1; the operating temperature in the first-stage air-flotation removal section 2A and the second-stage air-flotation removal section 4A is 80-88 ℃, and the operating pressure is 0.8-1.0 MPaG; the total retention time of the raw oil is 50 minutes, wherein the retention time in the first-stage air flotation removal section 2A is 25 minutes, and the retention time in the second-stage air flotation removal section 4A is 25 minutes.
Volume ratio (Nm) of ventilation to raw oil in high-air intake during desorption of suspended matter from filler3/h：m3The ratio of the first-stage air flotation removal section 2A to the second-stage air flotation removal section 4A to the second-stage air flotation removal section is 600:1, the operating temperature in the first-stage air flotation removal section 2A and the second-stage air flotation removal section 4A is 80-88 ℃, and the operating pressure is 0.4-0.5 MPaG; the total retention time of the carrying oil was 240 minutes, wherein the retention time in the first-stage air-flotation removal section 2A was 120 minutes, and the retention time in the second-stage air-flotation removal section 4A was 120 minutes.
The air-float gas in the above-mentioned processing procedure adopts nitrogen gas, and the microbubble generator adopts the micropore board, and the microbubble size that the controller formed through the micropore board is 50 μm.
The treated crude oil collected from the discharge port 10A is subjected to standing sedimentation for 24 hours to obtain an upper layer which is an oil phase and a lower layer which is a water phase, the oil-water separation interface is clear, the water content in the analyzed oil phase is 1.17-1.42%, the oil content in the water phase is 0.58-0.66%, 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 within about 10 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 11.0%, the oil content in the water phase was 5.62%, and the water phase contained a large amount of dark-black suspended matter.
Therefore, compared with the traditional air flotation filtration method, the method for removing the suspended matters has the advantages of keeping an ideal effect of removing the suspended matters and ensuring long-period operation, and particularly for heavy/poor oil products with high density, high viscosity and high content of the suspended matters, the suspended matters are difficult to remove, and the suspended matters removing has 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 (21)
1. The device for continuously removing suspended matters in crude oil comprises two sets of air floatation removing systems, wherein each set of air is provided with a gas inlet and a gas outletThe floatation removal system comprises at least two stages of floatation removal sections which are sequentially arranged from bottom to top, the lowest layer is a first-stage floatation removal section, floatation fillers are filled in the floatation removal sections, the fillers are low-density fillers, and the density is 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, the inlet of the micro-bubble generator is provided with a valve capable of controlling air flow or a plurality of valves with different air flow, and the inlet pipeline of the micro-bubble generator is provided with a pressurizing and air dissolving device and an air supplementing device; the top of the air floatation removal section at the uppermost layer is provided with a gas outlet which is connected with a gas-liquid separator, and the gas-liquid separator is connected with a pressurizing gas dissolving device; the bottom of the first-stage air floatation removal section is provided with a feed inlet, and the top of the uppermost air floatation removal section is provided with a discharge outlet.
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 continuously removing suspended matters from crude oil by using the device of any one of claims 1 to 4, after the crude oil to be treated is injected with water, the crude oil enters the device from a bottom feed inlet of a first-stage air floatation removal section of one set of air floatation removal system and is 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 higher porosity, larger blocks of suspended matters are adhered to the filler, the crude oil to be treated continuously and sequentially enters an upper air floatation removal section, the porosity of the filler is smaller and smaller, the suspended matters are removed step by step, and the treated crude oil is collected from a discharge port at the top of the uppermost air floatation removal section; the microbubble generator adopts low-air-volume air inlet, and the low-air-volume air inlet controls air inlet quantity to enable the filler in the air floatation removing section to make self-rotation motion without mutual collision; when filler absorption suspended solid in this air supporting desorption system is saturated, switch crude oil and carry out the suspended solid desorption by another set of air supporting desorption system feeding, and carry out the suspended solid desorption process in the filler with this set of air supporting desorption system, switch into carrying oil with the feeding, microbubble generator adopts high-capacity air admission simultaneously, high-capacity air admission is that control air input makes and takes place collision each other between the filler in the air supporting desorption section, make its absorbent suspended solid drop, is taken away by carrying oil, is collected by the discharge gate.
6. The method as claimed in claim 5, wherein the gas-bearing gas carries a small amount of liquid at the top of the uppermost gas-bearing removal section, the liquid 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 crude 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 carrier oil is selected from at least one of gasoline, kerosene, diesel oil, benzenes, esters, acids, ketones, and aldehyde organic solvents.
11. The method of claim 10, wherein the carrier oil is introduced continuously or intermittently.
12. The method of claim 5, wherein the gas introduced into the system is selected from nitrogen, air or an inert gas.
13. The method of claim 12, wherein the gas introduced into the system is nitrogen.
14. 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.
15. 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.
16. The method of claim 5, wherein the microbubble generator forms bubbles having a size of 50nm to 1000 μm.
17. The method of claim 16, wherein the microbubble generator forms bubbles having a size of 5 μm to 100 μm.
18. 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.
19. The process of claim 18, 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.
20. 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 0.5-500 minutes.
21. The method as claimed in claim 20, wherein the retention time of the oil to be treated in each stage of the air flotation removal section is 3-300 minutes.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201932927U (en) * | 2011-02-12 | 2011-08-17 | 天津瑞吉德科技有限公司 | Dissolved-gas type micro-vortex flow gas-floating oily sewage treatment device |
| 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 |
-
2018
- 2018-12-28 CN CN201811622905.7A patent/CN111378486B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201932927U (en) * | 2011-02-12 | 2011-08-17 | 天津瑞吉德科技有限公司 | Dissolved-gas type micro-vortex flow gas-floating oily sewage treatment device |
| 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 |
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