CN111378484A - Device and method for coupling crude oil suspended matter removal and oil-water separation - Google Patents
Device and method for coupling crude oil suspended matter removal and oil-water separation Download PDFInfo
- Publication number
- CN111378484A CN111378484A CN201811622906.1A CN201811622906A CN111378484A CN 111378484 A CN111378484 A CN 111378484A CN 201811622906 A CN201811622906 A CN 201811622906A CN 111378484 A CN111378484 A CN 111378484A
- Authority
- CN
- China
- Prior art keywords
- oil
- air flotation
- phase
- light
- flotation removal
- 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.)
- Granted
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 135
- 238000000926 separation method Methods 0.000 title claims abstract description 98
- 239000010779 crude oil Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims description 52
- 230000008878 coupling Effects 0.000 title claims description 12
- 238000010168 coupling process Methods 0.000 title claims description 12
- 238000005859 coupling reaction Methods 0.000 title claims description 12
- 238000005188 flotation Methods 0.000 claims abstract description 169
- 239000000945 filler Substances 0.000 claims abstract description 111
- 238000004581 coalescence Methods 0.000 claims abstract description 8
- 239000012071 phase Substances 0.000 claims description 212
- 239000003921 oil Substances 0.000 claims description 73
- 239000007789 gas Substances 0.000 claims description 58
- 239000000463 material Substances 0.000 claims description 20
- -1 polyethylene Polymers 0.000 claims description 20
- 238000012856 packing Methods 0.000 claims description 18
- 239000002657 fibrous material Substances 0.000 claims description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000004698 Polyethylene Substances 0.000 claims description 8
- 239000004743 Polypropylene Substances 0.000 claims description 8
- 229920000573 polyethylene Polymers 0.000 claims description 8
- 229920001155 polypropylene Polymers 0.000 claims description 8
- 230000002209 hydrophobic effect Effects 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 229920001778 nylon Polymers 0.000 claims description 5
- 229920000728 polyester Polymers 0.000 claims description 5
- 229920000915 polyvinyl chloride Polymers 0.000 claims description 5
- 239000004800 polyvinyl chloride Substances 0.000 claims description 5
- 239000004677 Nylon Substances 0.000 claims description 4
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 4
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 4
- 238000004381 surface treatment Methods 0.000 claims description 3
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 230000005661 hydrophobic surface Effects 0.000 claims description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 2
- 239000011261 inert gas Substances 0.000 claims description 2
- 229920000642 polymer Polymers 0.000 claims description 2
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 239000008346 aqueous phase Substances 0.000 claims 1
- 238000009941 weaving Methods 0.000 claims 1
- 238000010612 desalination reaction Methods 0.000 abstract description 4
- 239000003570 air Substances 0.000 description 144
- 238000011033 desalting Methods 0.000 description 28
- 239000000725 suspension Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 12
- 150000003839 salts Chemical class 0.000 description 12
- 238000007667 floating Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 238000001914 filtration Methods 0.000 description 7
- 230000014759 maintenance of location Effects 0.000 description 7
- 239000000835 fiber Substances 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- 230000005684 electric field Effects 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 3
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000004945 emulsification Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000265 homogenisation Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012212 insulator Substances 0.000 description 1
- WABPQHHGFIMREM-UHFFFAOYSA-N lead(0) Chemical compound [Pb] WABPQHHGFIMREM-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- 229920006306 polyurethane fiber Polymers 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The device comprises a light-phase air floatation removal system, an oil-water separation system and a heavy-phase air floatation removal system which are sequentially arranged from top to bottom and are communicated; the oil-water separation system is filled with coalescence separation filler, the light phase air floatation removal system comprises at least two stages of light phase air floatation removal sections, air floatation filler is filled in the light phase air floatation removal sections, and a bubble generator is arranged at the bottom of the light phase air floatation removal sections; the heavy phase air floatation removal system has the same structure. The device of the invention can realize the removal of suspended matters and oil-water separation of crude oil. The device has the advantages that suspended matters in crude oil are removed and oil-water deep separation is coupled into the whole treatment device, so that the suspended matters and the oil-water separation process are removed simultaneously and mutually promoted, the suspended matters can be efficiently removed, the oil-water deep separation is realized, the desalination is realized simultaneously, the air flotation filler can be prevented from being blocked or even blocked by the suspended matters, and the long-period efficient operation is ensured.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a device for coupling crude oil desalting and suspended matter removal and oil-water separation, and a method for removing suspended matter and separating oil from water by using the device.
Background
In recent years, with the trend of crude oil deterioration and heaviness strengthened, many crude oils contain a certain amount of suspended matters, which brings many problems to crude oil dehydration and desalination, oil-water separation and subsequent processing devices, and the main expression is as follows: (1) colloidal suspended matters in the crude oil are suspended in oil products, particularly in the crude oil in a flaky manner, so that the problems of equipment and pipelines flowing through the equipment, scaling of heating equipment, increase of system pressure drop and the like are easily caused; (2) the colloidal suspensions are not easy to be polarized in the traditional electric desalting process, so that the electric desalting effect is influenced, the salt content in the oil product subjected to electric desalting exceeds the standard, and the subsequent processing device is seriously corroded; (3) because colloid suspended matters are macromolecular substances, and the specific gravity of a plurality of suspended matters is in the range between oil and water, the colloid suspended matters are more suspended at an oil-water interface during oil-water separation, so that the oil-water separation interface is more turbid, the oil-water separation is difficult to realize, and the two separated phases are more seriously carried with each other; (4) the removal of these colloidal suspensions and the oil-water separation process are prone to filter clogging and coalescing material clogging by conventional methods (filtration, coalescing separation, etc.).
Crude oil in the prior art the pretreatment of crude oil in the prior art generally employs an electro-desalting process,
in the method, a small amount of water is firstly injected into the oil product to wash and dissolve the salts in the oil product, and then the oil-water separation is carried out by utilizing the electric desalting and dehydrating technology. At present, along with the quality of crude oil is more and more poor, the emulsification of oil is comparatively serious, and contains a large amount of suspended solids, leads to the not clear oil-water separation interface after the electric desalting dehydration, salt content index is unqualified, the oil water two-phase very serious scheduling problem of smuggleing mutually. Therefore, in order to achieve ideal effects of heavy and poor crude oil pretreatment (removal of suspended solids and oil-water separation (desalination)), new processes and equipment need to be developed to solve the problems of low oil-water separation efficiency, poor desalination effect, serious entrainment of oil-water phases and the like in the crude oil pretreatment process.
CN201310214820.6 proposes an electric desalting method and an electric desalting apparatus for crude oil, in which the first-stage electric desalting method for crude oil is to mix the crude oil to be desalted with a demulsifier without adding or adding only a small amount of washing water, then pour the mixture into an electric desalting tank at a proper temperature, further realize oil-water separation in the electric desalting tank, pass the separated oil through a filter located inside or outside the electric desalting tank to remove solid salt substances therein to obtain first-stage purified crude oil, and discharge the separated water after settling in the electric desalting tank. Due to the arrangement of the filter, solid salt substances in the crude oil do not need to be dissolved by using washing water any more, so that no washing water or only a small amount of washing water is added, the use amount of the washing water can be reduced or even cancelled, and the discharge amount of sewage is reduced. The method realizes the desalting and the de-solidification of the crude oil by the method of electric desalting and filtering, is inapplicable to heavy inferior crude oil and crude oil containing colloidal suspended matters, and has the problems of unqualified desalting index, easy blockage of filtering equipment and incomplete oil-water separation.
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.
In conclusion, if the pretreatment of the heavy and poor crude oil is to achieve a good effect, the suspended matter removal and oil-water separation effects are very important, because the suspended matter existence affects the oil-water separation effect, and the water existence in the material also affects the suspended matter removal effect, the efficiency of dewatering or suspended matter removal is reduced no matter the suspended matter is removed or the water is removed first, therefore, new processes and equipment need to be developed, the suspended matter removal and dewatering efficiency is greatly improved, and the problems that the suspended matter removal in the traditional process is not easy to deal with, the filtering equipment is easy to block, the oil-water two phases are serious to carry with each other and the like are solved.
Disclosure of Invention
Aiming at the problem that the process of removing suspended matters from crude oil and the process of oil-water separation in the prior art are mutually influenced to reduce the independent treatment efficiency to a certain extent, the invention provides the device and the method for coupling the removal of the suspended matters from the crude oil and the oil-water separation, which not only effectively remove the suspended matters in the crude oil, but also realize the deep separation of oil and water and improve the 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 coupling the suspended matter removal and oil-water separation of crude oil, which comprises a light-phase air flotation removal system, an oil-water separation system and a heavy-phase air flotation removal system which are sequentially arranged from top to bottom and are communicated;
the oil-water separation system comprises an oil-water separation filler layer, wherein a coalescence separation filler is filled in the oil-water separation filler layer, and a crude oil feeding hole to be treated is formed in the side surface of the oil-water separation filler layer;
the light-phase air flotation removal system comprises at least two stages of light-phase air flotation removal sections, the lowest layer is a first-stage light-phase air flotation removal section, air flotation fillers are filled in the light-phase air flotation removal sections, and the porosity of the fillers in the light-phase air flotation removal section on the upper layer is always smaller than the porosity of the fillers in the light-phase air flotation removal section on the lower layer; the bottom of each stage of light-phase air flotation removal section is provided with a bubble generator, and the top of the uppermost light-phase air flotation removal section is provided with a gas outlet and a treated light-phase outlet;
the heavy phase air flotation removal system comprises at least two stages of heavy phase air flotation removal sections, the uppermost layer is a first stage heavy phase air flotation removal section, air flotation fillers are filled in the heavy phase air flotation removal sections, and the porosity of the fillers in the heavy phase air flotation removal section on the upper layer is always larger than that of the fillers in the heavy phase air flotation removal section on the lower layer; the bottom of each stage of heavy phase air flotation removal section is provided with a bubble generator and is connected with an air inlet device, and the bottom of the heavy phase air flotation removal section at the lowest layer is provided with a treated heavy phase outlet.
Furthermore, the coalescence-separation filler in the oil-water separation filler layer is in a free loose-packed non-fixed state, is in a sheet shape, a rod shape, a spherical shape, a rectangular shape, a tetrahedral shape or a hexahedral shape, is formed by assembling an oleophylic hydrophobic fiber material and a hydrophilic oleophobic fiber material after being mixed and woven into an X-type, V-type, 8-type, omega-type, drop-shaped or diamond-shaped structure containing a compact concave-convex structure, and the ratio of the oleophylic hydrophobic fiber material to the hydrophilic oleophobic fiber material is 1: 1-1: 100, preferably 1: 2-1: 10. The oleophylic and hydrophobic fiber material is selected from at least one of polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic acid, nylon and materials with oleophylic and hydrophobic surface treatment, such as polyester fiber, nylon fiber, polyurethane fiber, polypropylene fiber, polyacrylonitrile fiber, polyvinyl chloride fiber and the like; the hydrophilic oleophobic fiber material is selected from natural high molecular polymers with carboxyl, amino or hydroxyl on the main chain or side chain or materials with hydrophilic oleophobic treatment on the surface, such as polypropylene fiber. The coalescence-separation filler is in a free bulk non-fixed state, and can be prevented from being blocked by suspended matters in the oil-water separation process.
Furthermore, the fillers in the light-phase air floatation removal system and the heavy-phase air floatation removal system are low-density fillers with the 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 filler may be of any shape, e.g. macroporous honeycomb filler, macroporous gauze fillerAny one type of material, hollow filler, fabric filler, and corrugated corner filler.
Furthermore, the porosity of the filler in the first-stage light-phase air flotation removal section and the first-stage heavy-phase air flotation removal section is 50-95%, and preferably 60-80%; the porosity of the filler in the light/heavy phase air floatation removal section at the uppermost layer is 10-50%, and the optimal porosity is 20-40%.
Further, the air flotation removal sections in the light-phase air flotation removal system and the heavy-phase air flotation removal system are arranged at 2-4 levels.
Further, the bubble generator is a device capable of generating micro-bubbles for use as the air flotation gas, and may be a combination of one or more devices, such as a single micro-bubble generator, or a combination of a distributor and an air dissolving device, all of which can achieve the purpose of providing micro-bubbles for the system. The distributor is selected from one of a tubular distributor, a sieve plate distributor, a bubble cap distributor and a grid distributor. The air dissolving device is selected from one or more combinations of a high-pressure air dissolving pump, a high-pressure jet pump and a pipeline air dissolving pump, and can be in a serial connection or a parallel connection when the air dissolving device is in multiple combinations; among them, a high-pressure air pump is preferable. The micro-bubble generator is selected from a micropore bubble generator, a membrane tube micro-disperser, an ultramicro-bubble generator and the like. As a more specific embodiment, the combination of the above devices provides the first stage light phase air flotation removal section and the first stage heavy phase air flotation removal section with air bubbles with the size of 0.01 mm-10 mm, preferably 0.1 mm-2 mm, and provides the other air flotation removal sections with air bubbles with the size of 50 nm-1000 μm, preferably 5 μm-100 μm.
Further, the gas collected from the top of the light-phase air flotation removal section at the uppermost layer returns to the system for recycling.
As will be understood by those skilled in the art, most of suspended matters in crude oil are lighter lipophilic substances, and most of the suspended matters enter a light-phase air flotation removal system along with a light phase, but because heavy inferior crude oil is seriously emulsified, an oil-water separation interface is unclear, and a small part of suspended matters enter a heavy phase, the suspended matters are removed from the light phase and the heavy phase; the method also considers the characteristic that suspended matters are easy to block the oil-water separation coalescence filler, adopts the filler in a free bulk non-fixed state, and enables the coalescence filler to move freely in a certain space in the oil-water separation process based on the buoyancy effect without blocking; the device of the invention utilizes the air flotation gas to remove suspended matters, mainly based on the dissolution characteristic of the gas in the liquid phase, after the air flotation gas is mixed with crude oil to be treated, micro bubbles of the gas are dispersed in the liquid, and the bubbles are adhered with the suspended matters and are adsorbed and attached by the filler of the air 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. In addition, the characteristics that the low-density bulk air-floating filler is easy to float and is not easy to block are utilized, so that the air-floating filler is in a floating state in an air-floating area, and the filler continuously moves and collides with each other in the process of adsorbing suspended matters, so that the suspended matters are uniformly attached to the inner surface and the outer surface of the filler to play a role in homogenization, and the air-floating filler is prevented from being blocked by the suspended matters and even blocked.
The technical purpose of the second aspect of the invention is to provide a method for performing suspended matter removal and oil-water separation coupling treatment on crude oil by using the device, the crude oil to be treated is injected with water and then fed from a side feed inlet of an oil-water separation system, deep separation of oil-water light phase and heavy phase is performed under the action of coalescence separation filler, the light phase upwards enters a light phase air flotation removal system and is mixed with bubbles generated by a bubble generator, the suspended matter floats upwards along with the bubbles, the filler in a first-stage light phase air flotation removal section has higher porosity, larger suspended matters are adhered to the filler, the light phase continuously upwards sequentially enters each stage of air flotation removal sections, the porosity of the filler is smaller and smaller, the suspended matters are removed step by step, the treated light phase is discharged from the light phase air flotation removal section at the uppermost layer, and gas is removed from a gas outlet at the top of the system; the heavy phase after oil-water separation downwards enters a heavy phase air flotation removal system and is mixed with bubbles generated by a bubble generator, suspended matters in the heavy phase air flotation removal system float upwards along with the bubbles, the filler in the first-stage heavy phase air flotation removal section has larger porosity, larger blocks of suspended matters are adhered to the filler, the heavy phase continuously and sequentially enters each stage of air flotation removal sections downwards, the porosity of the filler is smaller and smaller, the suspended matters are removed step by step, and the treated heavy phase is discharged from the heavy phase air flotation removal section at the bottommost layer.
Furthermore, the amount of water injected into the crude oil to be treated is 1-25% of the mass of the crude oil, and preferably 5-15%. In addition, as will be understood by those skilled in the art, through sufficient mixing and dissolution after water injection, the salt in the crude oil is dissolved in water, and the oil is desalted while removing suspended matters in the oil-water separation process.
Further, the gas floating gas used is selected from nitrogen, air or inert gas, preferably nitrogen.
Further, the operating conditions in the air flotation removal section of the light-phase air flotation removal system and the heavy-phase air flotation removal system are as follows: the temperature is normal temperature to 180 ℃, preferably 60 to 120 ℃; the pressure is 0.1 to 10.0MPa, preferably 1.0 to 5.0 MPa.
Further, the volume of the gas entering the first-stage light-phase air flotation removal section or the first-stage heavy-phase air flotation removal section is compared with the volume flow rate (Nm)3/h：m3The volume flow rate of the gas is 1: 1-1500: 1, preferably 100: 1-600: 1, and the volume flow rate of the gas is calculated by the volume of the gas in a standard state; the bubble size is 0.01mm to 10mm, preferably 0.1mm to 2 mm.
Further, the volume flow ratio (Nm) of the gas entering other air floatation removing sections to the raw oil3/h：m3The/h) is 1:1 to 500:1, preferably 2:1 to 100: 1. The bubble size is 50nm to 1000. mu.m, preferably 5 μm to 100. mu.m.
It should be understood by those skilled in the art that the ratio of the circulating gas of the secondary air-floatation removal system to the circulating gas of the primary air-floatation removal system can generally satisfy the above requirement range, and if a multi-stage air-floatation removal system is provided, the amount of gas in the higher-stage circulating air-floatation gas can be reduced, and then air can be supplemented by adding an air supplementing device.
In the above method, as a further preference, the total residence time of the oil phase in the air flotation removal section is 1 to 60 minutes, and preferably 5 to 30 minutes. The total retention time of the water phase in the air floatation removal section is 1-60 minutes, and preferably 3-15 minutes.
In the method, the crude oil to be treated is selected from any one of heavy inferior raw oil, heavy dirty oil, oily water containing desalted oil and coal tar.
In the above method, it should be understood by those skilled in the art that the treated light phase and heavy phase realize the removal of suspended matters and the deep separation of oil and water, the desalting is simultaneously completed in the separation process, the separated oil phase almost contains no suspended matters and water, the salt content index is qualified, the oil phase can directly enter the deep processing procedure of oil products, and the separated water phase also almost contains no suspended matters and oil components, and can be discharged to a sewage treatment unit.
Compared with the prior art, the invention has the following advantages:
(1) the device and the method couple the suspended substance removal and the oil-water deep separation in the crude oil into an integral processing device, so that the suspended substance removal and the oil-water separation processes are carried out simultaneously and mutually promoted, and the suspended substance removal and the oil-water deep separation can be realized efficiently.
(2) Because the existence of suspended matters influences the oil-water separation effect, and the existence of water in crude oil also influences the suspended matter removal effect, the device and the method of the invention greatly improve the suspended matter removal efficiency and the oil-water separation efficiency, and solve the problems of unsatisfactory suspended matter removal, easy blockage of filtering equipment, serious mutual entrainment of oil and water phases and the like in the traditional process.
(3) In the device, the oil-water separation filler layer is filled with free bulk non-fixed coalescence-separation filler, and when the material containing suspended matters is subjected to oil-water separation, the coalescence-separation filler can move freely in a certain space, so that a good coalescence-separation effect can be achieved, the coalescence-separation filler can be prevented from being blocked due to the adhesion and the attachment of the suspended matters, and a good basis is provided for realizing the coupling of suspended matter removal and oil-water deep separation.
(4) In the device, the air flotation removing section adopts low-density bulk air flotation fillers, so that the air flotation fillers are in a floating state in respective areas, and the fillers move continuously and collide with each other in the process of adsorbing suspended matters, so that the suspended matters are uniformly attached to the inner and outer surfaces of the fillers to play a role in homogenization, the air flotation fillers are prevented from being blocked or even dead by the suspended matters, and the long-period high-efficiency operation is ensured.
Drawings
FIG. 1 shows the apparatus for the separation of oil from water by the removal of suspended solids from crude oil in example 1.
The system comprises an oil-water separation system 100, a light phase air flotation removal system 200, a heavy phase air flotation removal system 300, an oil-water separation packing layer 101, a crude oil to be treated 102, a crude oil feeding port 201, a first-stage light phase air flotation removal section 202, a first-stage light phase air flotation packing layer 203, a second-stage light phase air flotation removal section 204, a second-stage light phase air flotation packing layer 205, a distributor I, 206, a micro-bubble generator I, 207, a gas outlet 208, a treated light phase outlet, 301, a first-stage heavy phase air flotation removal section, 302, a first-stage heavy phase air flotation packing layer, 303, a second-stage heavy phase air flotation removal section, 304, a second-stage heavy phase air flotation packing layer 305, a distributor II, 306, a micro-bubble generator II, 307, a treated heavy phase outlet, a 400, a gas compressor and a dissolved gas pump 500.
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
The device for coupling the crude oil suspended matter removal and the oil-water separation is shown in fig. 1 and comprises a light-phase air floatation removal system 200, an oil-water separation system 100 and a heavy-phase air floatation removal system 300 which are sequentially arranged from top to bottom and are communicated;
the oil-water separation system 100 comprises an oil-water separation filler layer 101, wherein a coalescence separation filler is filled in the oil-water separation filler layer, and a crude oil feeding hole 102 to be treated is formed in the side surface of the oil-water separation filler layer; the coalescence-separation filler is 8-type filler monomers with compact concave-convex structures, which are prepared by mixing polypropylene and polypropylene fibers according to a ratio of 1:2, and then the 8-type filler monomers are assembled into a rod-shaped filler with the length of 5mm, and the rod-shaped filler is filled in the oil-water separation filler layer 101 and is in a free loose-packed non-fixed state. The light-phase air flotation removal system 200 comprises two stages of light-phase air flotation removal sections, wherein the lower layer is a first-stage light-phase air flotation removal section 201, a first-stage light-phase air flotation filler layer 202 is arranged in the first-stage light-phase air flotation removal section, the polyethylene material macroporous honeycomb type filler is filled in the first-stage light-phase air flotation filler layer, and the porosity is 75-80%; the upper layer is a secondary light-phase air-flotation removal section 203, a secondary light-phase air-flotation filler layer 204 is arranged in the upper layer, and corrugated tooth-angle type fillers made of polyethylene materials are filled in the upper layer, wherein the porosity is 35-40%; the bottom of the first-stage light-phase air flotation filler layer 202 is provided with a distributor I205, and the front end of the distributor I205 is connected with the air inlet of a dissolved air pump 500; the bottom of the second-stage light-phase air-flotation packing layer 204 is provided with a micro-bubble generator I206, the front end of the micro-bubble generator I206 is connected with a gas compressor 400, the top of the second-stage light-phase air-flotation removing section 203 is provided with a gas outlet 207 and a treated light-phase outlet 208, the gas outlet 207 is connected with the gas compressor 400, and the air-flotation gas of the system is circulated to the micro-bubble generator I206 for reuse;
the heavy phase air flotation removal system 300 comprises two stages of heavy phase air flotation removal sections, wherein the upper layer is a first stage heavy phase air flotation removal section 301, a first stage heavy phase air flotation filler layer 302 is arranged in the first stage heavy phase air flotation removal section, the polyethylene material macroporous honeycomb type filler is filled in the first stage heavy phase air flotation filler layer, and the porosity is 75-80%; the lower layer is a second-stage heavy-phase air flotation removal section 303, a second-stage heavy-phase air flotation filler layer 304 is arranged in the lower layer, corrugated tooth angle type fillers made of polyethylene materials are filled in the lower layer, and the porosity is 35-40%; the bottom of the first-stage heavy-phase air flotation packing layer 302 is provided with a distributor II 305, and the front end of the distributor II 305 is connected with the air inlet of the dissolved air pump 500; the bottom of the second-stage heavy-phase air flotation packing layer 304 is provided with a micro-bubble generator II 306, the front end of the micro-bubble generator II 306 is connected with a gas compressor 400, and the bottom of the second-stage heavy-phase air flotation removing section 303 is provided with a treated heavy-phase outlet 307.
Example 2
The device for coupling the suspended matter removal of crude oil and the oil-water separation has the same structure and arrangement mode as those of the device in the embodiment 1 except that the porosity of the filler in the first-stage light-phase air flotation filler layer 202 and the first-stage heavy-phase air flotation filler layer 302 is 60-65%, and the porosity of the filler in the second-stage light-phase air flotation filler layer 204 and the second-stage heavy-phase air flotation filler layer 304 is 25-30%.
Example 3
The device for coupling the suspended matter removal of crude oil and the oil-water separation has the same structure and arrangement mode as those of the device in the embodiment 1 except that the porosity of the filler in the first-stage light-phase air flotation filler layer 202 and the first-stage heavy-phase air flotation filler layer 302 is 65-70%, and the porosity of the filler in the second-stage light-phase air flotation filler layer 204 and the second-stage heavy-phase air flotation filler layer 304 is 20-25%.
Example 4
The feedstock oil from a certain plant was processed by the apparatus of example 1, and the properties of the feedstock oil are shown in table 1, and the feedstock oil is a heavy crude oil and is characterized by high density, high viscosity, and severe emulsification.
TABLE 1
Injecting 5wt% of raw oil into water, feeding the raw oil from a raw oil inlet 102 to be treated on the side surface of an oil-water separation system 100, performing deep separation of oil-water light phase and heavy phase under the action of a cohesion separation filler in an oil-water separation filler layer 101, enabling the oil phase to upwards enter a light phase air flotation removal system 200 as a light phase, mixing the oil phase with bubbles (the size of the bubbles is 1-2 mm) cut by a dissolved air pump 500 and redistributed by a distributor I205 in a primary light phase air flotation removal section 201, enabling large suspended matters to float upwards along with the bubbles and adhere to the fillers, enabling the oil phase to continuously upwards enter a secondary light phase air flotation removal section 203 to be mixed with micro bubbles (the size of the bubbles is 50-100 mu m) generated by a micro bubble generator I206, enabling the remaining small suspended matters to be adsorbed to the fillers to be removed, discharging the treated oil phase from a treated light phase outlet 208, enabling air flotation gas to enter a gas compressor 400 from a gas outlet 207 at the, the compressed micro-bubble generator I206 is returned to be reused;
the water phase after oil-water separation enters the heavy phase air flotation removal system 300 downwards, the suspended matters in the water phase are removed through the same suspended matter removal process as the light phase air flotation removal system 200, and the treated water phase is discharged from a treated heavy phase outlet 307.
Air flotation removal of the light-phase air flotation removal system 200 and the heavy-phase air flotation removal system 300The operation temperature in the removing section is 85-90 ℃, and the operation pressure is 2.0-2.5 MPa; the volume flow ratio of the gas entering the first-stage light-phase air flotation removal section 201 (or the first-stage heavy-phase air flotation removal section 301) and the raw oil is controlled to be 400Nm3/h:1m3And/h, the volume flow ratio of the gas entering the secondary light-phase air flotation removal section 203 (or the secondary heavy-phase air flotation removal section 303) to the raw oil is 100:1, wherein the gas is calculated by the gas volume under the standard state.
The total retention time of the oil phase in the air flotation removal section is 8 minutes, and the total retention time of the water phase in the air flotation removal section is 6 minutes.
The air floating gas in the treatment process adopts nitrogen.
The salt content of the treated oil phase is 2.8-3.0 mg/L, the water content is 4200-5700 ppm, the oil content of the treated water phase is 0.32-0.46 wt%, suspended matters in the water phase and the oil phase are almost completely removed, and all packing layers of the device are not blocked in the operation process.
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 of the raw oil is 10 percent of the mass of the raw material;
the operating temperature in each air floatation removal section is 115-128 ℃, and the operating pressure is 1.5-2.0 MPa;
the sizes of the bubbles generated by the microbubble generator I206 and the microbubble generator II 306 are controlled to be 10-50 microns.
The volume flow ratio of the gas entering the first-stage light-phase air flotation removal section 201 (or the first-stage heavy-phase air flotation removal section 301) and the raw oil is controlled to be 180Nm3/h:1m3And/h, the volume flow ratio of the gas entering the secondary light-phase air flotation removal section 203 (or the secondary heavy-phase air flotation removal section 303) to the raw oil is 50:1, wherein the gas is calculated by the gas volume under the standard state.
The total retention time of the oil phase in the air flotation removal section is 12 minutes, and the total retention time of the water phase in the air flotation removal section is 8 minutes.
The salt content in the treated oil phase is 2.6-2.9 mg/L, the water content is 3500-4170 ppm, the oil content in the treated water phase is 0.28-0.31 wt%, suspended matters in the water phase and the oil phase are almost completely removed, and all packing layers of the device are not blocked in the operation process.
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 of the raw oil is 20 percent of the mass of the raw material;
the operating temperature in each air floatation removal section is 128-136 ℃, and the operating pressure is 2.0-2.5 MPa;
the bubble size generated by the distributor I205 and the distributor II 305 is controlled to be 0.1 mm-1 mm.
The sizes of the bubbles generated by the microbubble generator I206 and the microbubble generator II 306 are controlled to be 10-50 microns.
The volume flow ratio of the gas entering the first-stage light-phase air flotation removal section 201 (or the first-stage heavy-phase air flotation removal section 301) and the raw oil is controlled to be 600Nm3/h:1m3And/h, the volume flow ratio of the gas entering the secondary light-phase air flotation removal section 203 (or the secondary heavy-phase air flotation removal section 303) to the raw oil is 100:1, wherein the gas is calculated by the gas volume under the standard state.
The total retention time of the oil phase in the air flotation removal section is 20 minutes, and the total retention time of the water phase in the air flotation removal section is 14 minutes.
The salt content in the treated oil phase is 2.0-2.6 mg/L, the water content is 1200-1500 ppm, the oil content in the treated water phase is 0.08-0.17 wt%, suspended matters in the water phase and the oil phase are almost completely removed, and all packing layers are not blocked in the operation process of the device.
The conventional three-stage electric desalting method is adopted to remove suspended matters and separate oil from water in the crude oil of the table 1.
The three-stage electric desalting equipment is an electric desalting dehydrator and has the following structure: the horizontal structure is internally divided into an upper space and a lower space, the upper part is an electric field space, the lower part is an oil-water separation space, and the middle part is provided with a control section of a water-oil interface; in the electric field space there are several layers of horizontal electrode disks, suspension insulator, suspension plate, lead wire insulating rod, oil inlet nozzle and flowmeter. High voltage is transmitted to the electrode plates to form a high voltage electric field, and a weak electric field is formed between the lower electrode plate at the bottom of the dehydrator and the water boundary.
The operating conditions were as follows: operating temperature: 120-130 ℃; operating pressure: 0.8-1.2 MPaG; total residence time: 32 minutes; the total water injection amount is 15 percent of the mass of the raw oil.
After raw oil is desalted and dehydrated, the salt content of the obtained raw oil is 12.5-22.8 mg/L, the water content is 12800-17800 ppm, the oil content in sewage is 2.45-5.22 wt%, and the sewage is found to contain a large amount of blackish-black suspended substances.
Comparative example 2
The crude oil of the table 1 is desalted, dehydrated and suspended matter removed by adopting a method of four-stage electric desalting and a cyclone separator.
The four-stage electric desalting device is an electric desalting and dewatering device and has the same structure as the comparative example 1.
The operating conditions were as follows: operating temperature: 128-135 ℃; operating pressure: 0.8-1.2 MPaG; wherein the total residence time of the first three stages of electric desalting and dewatering devices is 32 minutes, and the total residence time of the fourth stage of electric desalting and dewatering devices is 32 minutes; the total water injection amount is 20 percent of the mass of the raw oil.
After raw oil is desalted and dehydrated, the salt content of the obtained raw oil is 8.8-10.2 mg/L, the water content is 7800-14580 ppm, the oil content in sewage is 2.43-4.55 wt%, and the sewage still contains a large amount of black and black suspended substances.
The experiments show that compared with the traditional electric desalting and dewatering technology, the device and the method have the advantages of good effects of desalting, removing suspended matters and separating oil from water simultaneously, the processes of removing the suspended matters and separating oil from water are carried out simultaneously and mutually promoted in the using process, the suspended matters can be removed efficiently, the deep separation of oil and water can be realized, the problems that the suspended matters influence the oil-water separation efficiency, the oil-water separation filler is easy to block, the oleophylic and hydrophilic properties of the surface of the filler are reduced and the like are solved, and the oil phase almost without the suspended matters and water and the water phase almost without the suspended matters and oil are obtained.
Claims (23)
1. A device for coupling the removal of suspended matters from crude oil and the separation of oil and water is characterized by comprising a light-phase air flotation removal system, an oil-water separation system and a heavy-phase air flotation removal system which are sequentially arranged from top to bottom and are communicated;
the oil-water separation system comprises an oil-water separation filler layer, wherein a coalescence separation filler is filled in the oil-water separation filler layer, and a crude oil feeding hole to be treated is formed in the side surface of the oil-water separation filler layer;
the light-phase air flotation removal system comprises at least two stages of light-phase air flotation removal sections, the lowest layer is a first-stage light-phase air flotation removal section, air flotation fillers are filled in the light-phase air flotation removal sections, and the porosity of the fillers in the light-phase air flotation removal section on the upper layer is always smaller than the porosity of the fillers in the light-phase air flotation removal section on the lower layer; the bottom of each stage of light-phase air flotation removal section is provided with a bubble generator, and the top of the uppermost light-phase air flotation removal section is provided with a gas outlet and a treated light-phase outlet;
the heavy phase air flotation removal system comprises at least two stages of heavy phase air flotation removal sections, the uppermost layer is a first stage heavy phase air flotation removal section, air flotation fillers are filled in the heavy phase air flotation removal sections, and the porosity of the fillers in the heavy phase air flotation removal section on the upper layer is always larger than that of the fillers in the heavy phase air flotation removal section on the lower layer; the bottom of each stage of heavy phase air flotation removal section is provided with a bubble generator and is connected with an air inlet device, and the bottom of the heavy phase air flotation removal section at the lowest layer is provided with a treated heavy phase outlet.
2. The apparatus of claim 1, wherein the coalescing separation packing within the de-oiling packing layer is in a free, bulk, non-set state.
3. The device according to claim 1, wherein the coalescence-separation filler is in a sheet shape, a rod shape, a spherical shape, a rectangular shape, a tetrahedral shape or a hexahedral shape, and is assembled by weaving an oleophilic hydrophobic fiber material and a hydrophilic oleophobic fiber material into an X-shaped, V-shaped, 8-shaped, Ω -shaped, drop-shaped or diamond-shaped structure having a dense uneven structure.
4. A device according to claim 3, wherein the ratio of oleophilic hydrophobic fibrous material to hydrophilic oleophobic fibrous material is from 1:1 to 1:100, preferably from 1:2 to 1: 10.
5. The device according to claim 3, wherein the oleophilic and hydrophobic fiber material is selected from at least one of polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic, nylon and materials with oleophilic and hydrophobic surface treatment, and the hydrophilic and oleophobic fiber material is selected from natural high molecular polymer with carboxyl, amino or hydroxyl on main chain or side chain or materials with hydrophilic and oleophobic surface treatment.
6. The apparatus of claim 1, wherein the packing material in the air flotation removal section is in an unfixed state.
7. The apparatus of claim 6, wherein the packing in the air flotation removal section is low density packing having a density of 50kg/m3～900kg/m3Preferably 300kg/m3～600kg/m3。
8. The device of claim 7, 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.
9. The apparatus as claimed in claim 1, wherein the porosity of the packing in the first stage light phase air-flotation removal section and the first stage heavy phase air-flotation removal section is 50-95%.
10. The apparatus of claim 1, wherein the porosity of the packing in the uppermost light/heavy gas flotation removal section is in the range of 10% to 50%.
11. The device as claimed in claim 1, wherein the flotation removal sections of the light-phase and heavy-phase flotation removal systems are arranged in 2-4 stages.
12. The apparatus as claimed in claim 1, wherein the bubble generator is an apparatus capable of generating micro-bubbles for use as the air-bearing gas, and supplies bubbles having a size of 0.01mm to 10mm to the first-stage light-phase air-bearing removal section and the first-stage heavy-phase air-bearing removal section, and supplies bubbles having a size of 50nm to 1000 μm to the other air-bearing removal sections.
13. The apparatus of claim 1, wherein the gas collected from the top of the uppermost light-phase gas flotation removal section is returned to the system for recycling.
14. The method for performing suspended matter removal and oil-water separation coupling treatment on crude oil by using the device of any one of claims 1 to 13, after the crude oil to be treated is injected with water, feeding the crude oil through a side feed inlet of an oil-water separation system, performing deep separation of an oil-water light phase and a heavy phase under the action of coalescence separation filler, enabling the light phase to upwards enter a light phase air flotation removal system and be mixed with bubbles generated by a bubble generator, wherein the suspended matters float upwards along with the bubbles, the filler in a first-stage light phase air flotation removal section has higher porosity, enabling larger suspended matters to be adhered to the filler, enabling the light phase to continuously upwards and sequentially enter each stage of air flotation removal sections, enabling the porosity of the filler to be smaller and smaller, removing the suspended matters step by step, discharging the treated light phase from a light phase air flotation section at the uppermost layer, and removing gas from a gas outlet; the heavy phase after oil-water separation downwards enters a heavy phase air flotation removal system and is mixed with bubbles generated by a bubble generator, suspended matters in the heavy phase air flotation removal system float upwards along with the bubbles, the filler in the first-stage heavy phase air flotation removal section has larger porosity, larger blocks of suspended matters are adhered to the filler, the heavy phase continuously and sequentially enters each stage of air flotation removal sections downwards, the porosity of the filler is smaller and smaller, the suspended matters are removed step by step, and the treated heavy phase is discharged from the heavy phase air flotation removal section at the bottommost layer.
15. The method of claim 14, wherein the water is injected into the crude oil to be treated in an amount of 1% to 25% by mass of the crude oil.
16. The process according to claim 14, wherein the gas-flotation gas used in the gas-flotation removal section is selected from nitrogen, air or an inert gas, preferably nitrogen.
17. The method according to claim 14, wherein the volume flow ratio of the gas volume entering the first-stage light-phase air flotation removal section or the first-stage heavy-phase air flotation removal section to the raw oil is 1: 1-1500: 1.
18. The method as claimed in claim 17, wherein the size of the bubbles entering the first-stage light-phase air-flotation removal section or the first-stage heavy-phase air-flotation removal section is 0.01 mm-10 mm.
19. The method as claimed in claim 17, wherein the volume flow ratio of the gas entering other air flotation removal sections to the raw oil is 500: 1-1: 1.
20. The method as claimed in claim 19, wherein the size of the bubbles entering the other air flotation removal section is 50nm to 1000 μm.
21. The process of claim 14, wherein the operating conditions in the gas removal sections of the light phase gas removal system and the heavy phase gas removal system are as follows: the temperature is normal temperature to 180 ℃, and the pressure is 0.3 to 10.0 MPa.
22. The method according to claim 14, wherein the total residence time of the oil phase in the air flotation removal section is 1 to 60 minutes, preferably 5 to 30 minutes.
23. The process according to claim 14, wherein the total residence time of the aqueous phase in the air flotation removal section is 1 to 60 minutes, preferably 3 to 15 minutes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811622906.1A CN111378484B (en) | 2018-12-28 | 2018-12-28 | Device and method for coupling crude oil suspended matter removal and oil-water separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811622906.1A CN111378484B (en) | 2018-12-28 | 2018-12-28 | Device and method for coupling crude oil suspended matter removal and oil-water separation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111378484A true CN111378484A (en) | 2020-07-07 |
| CN111378484B CN111378484B (en) | 2021-07-09 |
Family
ID=71216302
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811622906.1A Active CN111378484B (en) | 2018-12-28 | 2018-12-28 | Device and method for coupling crude oil suspended matter removal and oil-water separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111378484B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN106823470A (en) * | 2017-01-12 | 2017-06-13 | 华东理工大学 | A kind of compound coalescence material for water de-oiling |
| CN109019913A (en) * | 2018-08-08 | 2018-12-18 | 青岛三油气科技有限责任公司 | A kind of compact separation method of Oil Field of oil removing oil removal |
-
2018
- 2018-12-28 CN CN201811622906.1A patent/CN111378484B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN106823470A (en) * | 2017-01-12 | 2017-06-13 | 华东理工大学 | A kind of compound coalescence material for water de-oiling |
| CN109019913A (en) * | 2018-08-08 | 2018-12-18 | 青岛三油气科技有限责任公司 | A kind of compact separation method of Oil Field of oil removing oil removal |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111378484B (en) | 2021-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109652117B (en) | Oil-water separation system and separation process method | |
| CN109652118B (en) | Washing desalination and oil-water separation process system and process method | |
| US7635435B2 (en) | Method and apparatus for oil water separation | |
| 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 | |
| WO2016127273A1 (en) | Method and apparatus for strengthening oil-water separation and coupled desalting functions in cold low pressure separator | |
| US20080035586A1 (en) | Enhanced coalescer | |
| CN109652119B (en) | Dirty oil/aging oil treatment equipment | |
| CN112499733B (en) | O/W emulsion demulsification and oil removal device and method based on electric field synergistic medium coalescence | |
| CN110980981A (en) | Deep purification device and purification method for methanol-to-olefin washing water | |
| WO2022116899A1 (en) | Method and device for enhancing oil dehydration by means of synergy of electric field and medium coalescence | |
| CN111378484B (en) | Device and method for coupling crude oil suspended matter removal and oil-water separation | |
| CN111378485B (en) | Pretreatment device and method for crude oil desalting and colloid removing suspended matter | |
| CN111378488B (en) | Crude oil pretreatment device and method | |
| CN114702095B (en) | Circulating oil-water separation system and method for coupling segmented fiber particles with microbubbles | |
| CN112745904B (en) | Device and method for removing suspended matters and deeply dewatering oil | |
| CN112745910B (en) | Suspended matter removal and oil-water separation coupling device and method | |
| CN111303931B (en) | Heavy dirty oil dehydration method | |
| CN204569838U (en) | NSF diesel oil coalescer | |
| CN211664891U (en) | Deep purification device for methanol-to-olefin washing water | |
| US20110042288A1 (en) | Enhanced Coalescer | |
| CN211688517U (en) | Process water treatment system of ethylene production device by ethylene-propylene-alkane mixed steam cracking | |
| CN216837238U (en) | Complete equipment for classification, coalescence and oil removal of coal tar desalted sewage | |
| CN111378486B (en) | Device and method for continuously removing suspended matters in crude oil | |
| CN111378487B (en) | Device and method for removing suspended matters in oil products |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231018 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |