CN111378485B - Pretreatment device and method for crude oil desalting and colloid removing suspended matter - Google Patents
Pretreatment device and method for crude oil desalting and colloid removing suspended matter Download PDFInfo
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- CN111378485B CN111378485B CN201811622894.2A CN201811622894A CN111378485B CN 111378485 B CN111378485 B CN 111378485B CN 201811622894 A CN201811622894 A CN 201811622894A CN 111378485 B CN111378485 B CN 111378485B
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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
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- 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 a sedimentation system, a first-stage air floatation removal system and at least one second-stage air floatation removal system; the I-level air floatation removal system comprises a packing layer I, an air dissolving device and an air supplementing device, and the II-level air floatation removal system comprises a packing layer II, a gas-liquid separator, a supercharging device and a micro-bubble generator. By adopting the device, the air floatation removing system utilizes air floatation gas to adhere colloid suspended matters and is hung and removed by the packing layer, and the preliminary coarse separation of oil and water is realized. The removal of salt and colloid suspended matters in the crude oil is coupled into an integral processing device, so that the desalting and colloid suspended matters and the colloid suspended matters are synchronously carried out, and the processing efficiency is high; provides a good foundation for the subsequent coalescence-separation treatment of the crude oil.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a pretreatment device for desalting crude oil and removing colloidal suspended matters, and a method for desalting crude oil and removing colloidal suspended matters by using the pretreatment device.
Background
The crude oil contains water and salts such as sodium chloride, calcium chloride, magnesium chloride and the like, and in order not to 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 a refinery with residual oil hydrogenation or heavy oil cracking are more strict, and the salt content in the crude oil is less than 3 mg/L. The main reason is that the salt and water contained in the crude oil cause great harm to the storage, transportation, processing, product quality, equipment and the like of the crude oil, such as increasing the load of the storage, transportation and processing equipment, influencing the normal operation of a distillation device, corroding equipment, poisoning catalysts and influencing the quality of secondary processing oil products.
In recent years, with the trend of crude oil deterioration and heaviness strengthened, more crude oil contains a certain amount of colloidal suspended matters, which brings more problems to the crude oil dehydration and desalination process and the subsequent processing device, and the main expression 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.
Crude oil treatment in the prior art generally comprises dehydration and desalination: firstly, a small amount of water is injected into the oil product to wash and dissolve the salt in the oil product, and then the brine is separated by utilizing the electric desalting and dewatering technology, so that the following problems exist: (1) the colloid suspended matters can not be removed in the electric desalting process, so that the salt content index in the desalted crude oil is unqualified; (2) the colloid suspended substance affects the oil-water separation effect, so that oil and water are very seriously carried by each other. These colloidal suspensions are disadvantageous in either oil or sewage and require removal followed by oil-water separation.
In the prior art, crude oil dehydration and desalination generally adopts an electric desalting method, a small amount of water is firstly injected into oil products to wash and dissolve salt in the oil products, and then brine is separated by using an electric desalting and dehydration technology, and the method has the following problems: (1) the colloid suspended matters can not be removed in the electric desalting process, so that the salt content index in the desalted crude oil is unqualified; (2) the colloid suspended substance affects the oil-water separation effect, so that oil and water are very seriously carried by each other. Therefore, if a heavy and poor crude oil pretreatment (desalting, removing suspended solids and separating oil from water) process needs to be realized, new processes and equipment need to be developed, and the problems of unsatisfactory technical indexes, poor desalting effect, serious mutual entrainment of oil and water phases and the like in the oil product dehydration and desalting process are solved.
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.
To sum up, in order to realize the treatment of heavy and poor crude oil, the removal of colloidal suspended solids is an important part, and new processes and equipment need to be developed so as to solve the problems that the traditional processes in the prior art are easy to cause the blockage of filtering equipment, and oil and water phases are seriously entrained with each other.
Disclosure of Invention
Aiming at the defect of lack of equipment capable of effectively removing salt and colloid suspended matters in crude oil in the prior art, the invention provides the pretreatment device and the pretreatment method for desalting and removing the colloid suspended matters from the crude oil, which have good effects of desalting and removing the colloid suspended matters and have high treatment efficiency.
The technical purpose of the invention is realized by the following technical means:
the technical purpose of the first aspect of the invention is to provide a pretreatment device for crude oil desalting and colloid suspended substance removal, which comprises a sedimentation system, a first-stage air floatation removal system and at least one second-stage air floatation removal system which are sequentially connected from bottom to top;
the settling system comprises a liquid containing device with an open top, and an inlet and an outlet are respectively arranged on the side surface and the bottom of the upper part of the liquid containing device; the inlet is a tangential feed inlet; the top of the liquid accommodating device is open and is communicated with the I-level air floatation removal system;
the I-stage air floatation removal system comprises a packing layer I, wherein an outlet is arranged on the side edge above the packing layer I and is connected with an air dissolving device, the air dissolving device is connected to the bottom of the packing layer I, and an air supplementing device is further arranged at the front end of the air dissolving device;
the second-level air floatation removal system comprises a packing layer II, a gas-liquid separator, a supercharging device and a micro-bubble generator, wherein an outlet is arranged on the side edge above the packing layer II and connected with the supercharging device, the supercharging device is connected with the micro-bubble generator, and the micro-bubble generator is arranged at the bottom of the packing layer II;
and the liquid accommodating device, the packing layer I of the I-level air floatation removal system and the packing layer II of the II-level air floatation removal system are sequentially communicated from bottom to top.
Further, in the above apparatus, the liquid container is a container having any shape or any combination of shapes that can provide a space for crude oil to settle, and particularly preferably a container having a cylindrical upper part and an inverted conical lower part; the cone angle of the inverted cone-shaped part is 3-40 degrees, and preferably 5-15 degrees.
Furthermore, in the above device, the tangential feed inlets of the liquid container are arranged in a plurality of, preferably symmetrically distributed, and have a structure that enables the feed to reach a high rotational flow state, so as to realize rapid coarse separation of the light and heavy phases, and the inverted cone structure at the lower part of the liquid container is also beneficial to accelerating the rotational flow of the material, so as to realize separation.
Furthermore, in the above device, the I-stage air flotation removal system further comprises a distributor, which is arranged between the packing layer I and the air dissolving device, is positioned at the bottom of the packing layer I, and is used for redistributing the materials of the air dissolving device into the packing layer I, so that the materials are distributed more uniformly and are more fully contacted with the packing layer I. More specifically, the distributor is selected from one of a pipe distributor, a sieve plate distributor, a bubble cap distributor and a grid distributor.
Further, in the above device, 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 when the air dissolving device is a plurality of combinations, the air dissolving device can be in a serial connection or a parallel connection; among them, a high-pressure air pump is preferable. The selection or combination mode of the gas dissolving device is required to form bubbles with the size of 0.01 mm-10 mm, preferably 0.1 mm-2 mm by cutting gas and liquid.
Further, in the above device, the filler layer i and the filler layer ii are of a porous structure composed of lipophilic materials having lipophilic functions, and the lipophilic materials are at least one selected from polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic, nylon and materials having lipophilic surfaces. The oleophilic material can be in any shape, such as honeycomb type packing, silk screen type packing, hollow type packing, fabric type packing and corrugated tooth angle type packing, and the porosity of the packing layer I is 50-95%, preferably 60-80%. The packing layer II has smaller porosity which is 10-50%, preferably 20-40%.
Generally, the lower porosity is beneficial to adhering and hanging more large colloidal suspended matters, but the larger porosity causes the penetration of the smaller colloidal suspended matters, and the removal is not thorough, so that the device of the invention is provided with the larger porosity at the packing layer I of the I-grade air floatation removal system to remove the larger colloidal suspended matters, and is provided with the smaller porosity at the packing layer II of the II-grade air floatation removal system to further remove the residual colloidal suspended matters with smaller sizes.
Further, in the above apparatus, the pressure increasing means is a gas compressor.
Further, in the above device, the second-stage air floatation removal system further comprises an air supply device arranged at the front end of the supercharging device.
Further, in the above apparatus, the microbubble generator may be an apparatus capable of dispersing gas into a smaller size than the gas dissolving apparatus, or may be referred to as a micro bubble generator, a membrane tube micro disperser, an ultra micro bubble generator, or the like, and may form bubbles having a size of 50nm to 1000 μm, preferably 5 μm to 100 μm, and any apparatus capable of realizing the above functions may be used in the present invention.
The technical purpose of the second aspect of the invention is to provide a pretreatment method for desalting and removing suspended matters from crude oil by using the device, after water is injected into the crude oil to be treated and the crude oil is fully dissolved and mixed, feeding the crude oil from an inlet of a liquid accommodating device, forming a rotational flow by feeding to generate separation of a light phase and a heavy phase, discharging the heavy phase from an outlet at the bottom of the liquid accommodating device, enabling colloidal suspended matters to float upwards along with the light phase to enter a first-stage air floatation removal system, mixing micro bubbles cut by an air dissolving device with crude oil to be treated to enter a packing layer I, enabling the bubbles to carry the colloidal suspended matters to be adsorbed and hung by packing materials in the packing layer I, enabling the packing layer I to have high porosity to remove large colloidal suspended matters, enabling part of gas to carry part of crude oil feed liquid to enter the air dissolving device through a pipeline from the side edge above the packing layer I for recycling, and supplementing insufficient gas by a gas;
the light-phase material with the large colloid suspended matters removed continues to upwards enter a II-level air floatation removal system and is mixed with micro bubbles generated by a micro bubble generator to enter a packing layer II, the packing layer II has smaller porosity, so that the residual small colloid suspended matters can be removed, gas enters a gas-liquid separator from an outlet at the side edge above the packing layer II, the separated gas enters a supercharging device to be supercharged and then is conveyed to the micro bubble generator to be recycled, and the treated light-phase material is discharged from the top of the packing layer II.
In the above method, it should be understood by those skilled in the art that the two streams of the discharged materials from the top and the bottom of the above apparatus achieve the coarse separation of oil and water and the removal of colloidal suspended substances, and the separated materials can respectively continue to pass through the subsequent methods of crude oil coalescence-removal treatment, etc. to achieve the complete separation of oil and water, and achieve more complete desalting.
In the method, the amount of water injected into the crude oil to be treated is 3-20% of the mass of the crude oil. After sufficient dissolution and mixing, the salt in the crude oil is dissolved in the water phase, and then the crude oil is roughly separated by a settling system.
In the above method, as will be understood by those skilled in the art, most of colloid suspended matters in crude oil are lighter lipophilic substances, and enter the I-stage air-flotation removal system along with the separation of light phase and heavy phase.
In the method, the gas used in the first-stage air flotation removal system and the second-stage air flotation removal system is selected from nitrogen, air or inert gas, and preferably nitrogen.
In the method, the operating parameters of the I-stage air floatation removal system are as follows: the temperature is normal temperature to 180 ℃, preferably 60 to 120 ℃; the pressure is 0.3 to 10.0MPa, preferably 2.0 to 5.0 MPa.
In the above method, the gas-dissolving device may have a volume flow ratio (Nm) of gas to feedstock oil3/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 insufficient gas is supplemented by a gas supplementing device. The size of the bubbles formed by cutting by the dissolved air device in the I-stage air floatation removal system is 0.01 mm-10 mm, preferably 0.1 mm-2 mm.
In the method, the operating parameters of the II-stage air floatation 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 2.0 to 5.0 MPa.
In the above method, the ratio of the gas volume flow rate in the pressurizing means to the gas volume flow rate of the gas dissolving means (Nm)3/h：Nm3The/h) is 1:500 to 1:1, preferably 1:20 to 1: 2. The size of bubbles formed by the micro-bubble generator provided with the II-level air floatation removal system is 50 nm-1000 μm, and preferably 5 μm-100 μm.
It should be understood by those skilled in the art that the circulating air-flotation gas of the secondary air-flotation removal system is derived from the air-flotation removal system of the previous stage, and the ratio thereof generally satisfies the above-mentioned requirement range, and if a multi-stage air-flotation removal system is provided, the amount of gas in the higher-stage circulating air-flotation gas may be reduced, and then the air can be supplemented by providing an air supplementing device.
It will be appreciated by those skilled in the art that the packing in the apparatus will become saturated during use and may be replaced or backwashed to continue operation.
Compared with the prior art, the invention has the advantages that:
(1) the device and the method can effectively remove the salt and the colloid suspended matters in the crude oil, and couple the removal of the salt and the colloid suspended matters in the crude oil into an integral processing device, so that the desalting and the colloid suspended matters are synchronously carried out, and the processing efficiency is high;
(2) in the prior art, most of the devices and the methods adopt an electro-desalting technology, colloid suspended matters are not easy to be polarized in the traditional electro-desalting process, flow through equipment and pipelines are easy to block, the desalting effect is influenced, oil-water separation is difficult to realize, the oil-water separation is incomplete, two phases are seriously carried mutually.
Drawings
FIG. 1 is a pretreatment apparatus for desalting and degumming a suspension of crude oil.
The system comprises a liquid tank 101, a liquid tank 102, a liquid tank inlet 103, a liquid tank outlet 201, a packing layer I, a packing layer 202, a first-stage air floatation removal system outlet 203, an air supply device 204, a high-pressure dissolved air pump 205, a tubular distributor 301, a packing layer II, a packing layer 302, a gas-liquid separator 303, a gas compressor 304 and a micro-bubble generator.
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 pretreatment device for crude oil desalting and colloid removing suspended matters comprises a sedimentation system, a first-stage air floatation removing system and a second-stage air floatation removing system which are sequentially connected from bottom to top as shown in figure 1; the settling system comprises a liquid tank 101 with an open top, a cylindrical upper part and an inverted cone-shaped lower part, wherein the cone angle of the inverted cone-shaped part is 12 degrees, and a liquid tank inlet 102 and a liquid tank outlet 103 are respectively arranged on the side surface of the cylindrical upper part and the bottom of the inverted cone; the liquid tank inlet 102 is a tangential feed inlet; the top of the liquid tank 101 is open and is communicated with a first-stage air floatation removal system; the I-stage air floatation removal system comprises a packing layer I201, wherein an I-stage air floatation removal system outlet 202 is arranged on the side edge above the packing layer I201 and is connected with a high-pressure dissolved air pump 204, the high-pressure dissolved air pump 204 is connected with a tubular distributor 205 and is arranged at the bottom of the packing layer I201, and an air supplement device 203 is further arranged at the front end of the high-pressure dissolved air pump 204; the II-level air floatation removal system comprises a packing layer II 301, a gas-liquid separator 302, a gas compressor 303 and a micro-bubble generator 304, wherein the gas-liquid separator 302 is arranged above the packing layer II 301 and connected with the gas compressor 303, the gas compressor 303 is connected with the micro-bubble generator 304, and the micro-bubble generator 304 is arranged at the bottom of the packing layer II 301; the liquid tank 101, the packing layer I201 and the packing layer II 301 are communicated in sequence from bottom to top.
In the device, the filler layer I201 is a polyethylene macroporous honeycomb type filler, the porosity is 75-80%, the filler layer II 301 is a polyethylene corrugated tooth angle type filler, and the porosity is 35-40%.
Example 2
In the pretreatment device for crude oil desalting and colloid removing suspended matters, a liquid tank inlet 102 is provided with two symmetrical tangential feed inlets, the cone angle of an inverted cone part is 8 degrees, the porosity of a packing layer I201 is 60-65 percent, the porosity of a packing layer II 301 is 25-30 percent, and other structures and arrangement modes are the same as those in embodiment 1.
Example 3
In the pretreatment device for crude oil desalting and colloid removing suspended matters, four symmetrical tangential feed inlets are arranged at an inlet of a liquid tank, the cone angle of an inverted cone part is 5 degrees, the porosity of a packing layer I201 is 65-70 percent, the porosity of a packing layer II 301 is 30-35 percent, and other structures and arrangement modes are the same as those in example 1.
Example 4
The apparatus of example 1 was used to desalt and degum suspended material from a feedstock oil from a plant, which had properties shown in table 1 and was a heavy crude oil characterized by high density, high viscosity and severe emulsification.
TABLE 1
Injecting water into the crude oil and fully mixing, wherein the water injection amount is 15% of the mass of the crude oil, feeding the crude oil from a liquid tank inlet 102, forming cyclone during feeding and separating a light phase from a heavy phase because the liquid tank inlet 102 is a tangential feed inlet, discharging the heavy phase from a liquid tank outlet 103, enabling colloidal suspended matters to upwards float along with the light phase to enter a I-grade air floatation removal system, enabling the operating parameters of the I-grade air floatation removal system to be 85-90 ℃ and 2.0-2.5 MPa, mixing nitrogen micro-bubbles cut by a high-pressure air dissolving pump 204 with the crude oil to be treated to enter a packing layer I201, and enabling the volume flow ratio of gas to the crude oil in the high-pressure air dissolving pump 204 to be 300Nm3/h:1m3The size of the formed bubbles is 1 mm-2 mm; bubbles carrying colloidal suspended matters are adsorbed and attached by the filler in the filler layer I201, the filler layer I201 has high porosity, large colloidal suspended matters are removed, part of gas carrying a small amount of crude oil feed liquid enters a high-pressure gas dissolving pump 204 from an outlet 202 of the I-level air floatation removal system for recycling through a pipeline, and insufficient gas is supplemented by a gas supplementing device 203;
the light-phase material with the large colloid suspended substances removed continuously enters a II-level air-flotation removal system upwards, the operating parameters of the II-level air-flotation removal system are that the temperature is 85-90 ℃, the pressure is 2.0-2.5 MPa, the material is mixed with micro bubbles (50-100 mu m) generated by a micro-bubble generator 304 and enters a packing layer II 301, the packing layer II 301 has smaller porosity, so that the residual small colloid suspended substances can be removed, part of gas carries a small amount of crude oil feed liquid and enters a gas-liquid separator 302, the separated gas is pressurized by a gas compressor 303 and then is conveyed to the micro-bubble generator 304 for recycling, the volume flow ratio of the gas in the gas compressor 303 to the gas in a high-pressure gas dissolving pump 204 is 1Nm, and the volume flow ratio3/h:10Nm3And h, discharging the treated light-phase material from the top of the packing layer II 301.
The salt content of the treated crude oil is 4.6-7.5 mg/L, the water content is 8700-12800 ppm, the oil content in the sewage is 0.68-0.94 wt%, and most of suspended matters in the sewage are removed.
Example 5
The crude oil from the same source as above was processed using the apparatus of example 2, with the water injection amount of crude oil before feeding being 8% of the mass of the crude oil, and the volumetric flow ratio of gas to crude oil in the high pressure gas pump 204 being 150Nm3/h:1m3The size of the micro-bubbles generated by the micro-bubble generator 304 is 10-50 μm, and the volume flow ratio of the gas in the gas compressor 303 to the gas in the high-pressure gas dissolving pump 204 is 1Nm3/h:5Nm3The other operating conditions were as in example 4.
The salt content of the treated crude oil is 3.5-6.8 mg/L, the water content is 7800-11500 ppm, the oil content in the sewage is 0.45-0.87 wt%, and suspended matters in the sewage are completely removed.
Example 6
The crude oil from the same source as above was processed using the apparatus of example 3, with the water injection amount of crude oil before feeding being 17% of the mass of the crude oil, and the volumetric flow ratio of gas to crude oil in the high pressure gas pump 204 being 400Nm3/h:1m3The size of the formed bubbles is 0.1 mm-1 mm; the size of the micro-bubbles generated by the micro-bubble generator 304 is 10-50 μm, and the gas compressorThe volume flow ratio of the gas in the high-pressure gas dissolving pump 204 to the gas in the gas tank 303 is 1Nm3/h:2Nm3The other operating conditions were as in example 4.
The salt content of the treated crude oil is 2.2-2.8 mg/L, the water content is 3200-5500 ppm, the oil content in the sewage is 0.17-0.32 wt%, and suspended matters in the sewage are completely removed.
Comparative example 1
The crude oil of table 1 is desalted, dehydrated and suspended substance removed by adopting a conventional three-stage electric desalting method.
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: 125-130 ℃; operating pressure: 0.8-1.2 MPaG; total residence time: 36 minutes; the total water injection amount is 17 percent of the mass of the raw oil.
After raw oil is desalted and dehydrated, the salt content of the obtained raw oil is 12.3-21.7 mg/L, the water content is 12500-16400 ppm, the oil content in sewage is 2.54-5.76 wt%, and the sewage is found to contain a large amount of black and 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: 125-130 ℃; operating pressure: 0.8-1.2 MPaG; wherein the total residence time of the first three stages of electric desalting and dewatering devices is 36 minutes, and the total residence time of the fourth stage of electric desalting and dewatering devices is 36 minutes; the total water injection amount is 25 percent of the mass of the raw oil.
After raw oil is desalted and dehydrated, the salt content of the obtained raw oil is 8.1-9.8 mg/L, the water content is 7500-12200 ppm, the oil content in sewage is 2.20-4.51 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 effect of desalting and removing suspended matters simultaneously, and especially for heavy/poor oil products with high density, high viscosity, serious emulsification and high salt content, the problems of high salt content, more suspended matters, large amount of oil and water, high oil content in water and the like in the treated raw oil can be caused due to the fact that desalting and removing suspended matters are difficult and the suspended matters exist and have great influence on desalting and dewatering.
Claims (23)
1. The pretreatment device for crude oil desalting and colloid removing suspended matters is characterized by comprising a sedimentation system, a first-stage air floatation removal system and at least one second-stage air floatation removal system which are sequentially connected from bottom to top;
the settling system comprises a liquid containing device with an open top, and an inlet and an outlet are respectively arranged on the side surface and the bottom of the upper part of the liquid containing device; the inlet is a tangential feed inlet; the top of the liquid accommodating device is open and is communicated with the I-level air floatation removal system;
the I-stage air floatation removal system comprises a packing layer I, the porosity of the packing layer I is 50% -95%, an outlet is arranged on the side edge above the packing layer I and connected with an air dissolving device, the air dissolving device is connected to the bottom of the packing layer I, and an air supplementing device is further arranged at the front end of the air dissolving device;
the II-level air flotation removal system comprises a packing layer II, a gas-liquid separator, a supercharging device and a micro-bubble generator, the porosity of the packing layer II is 10% -50%, an outlet is formed in the side edge above the packing layer II and is connected with the supercharging device, the supercharging device is connected with the micro-bubble generator, the micro-bubble generator is arranged at the bottom of the packing layer II, and the micro-bubble generator is a device for forming bubbles with the size of 50 nm-1000 microns;
and the liquid accommodating device, the packing layer I of the I-level air floatation removal system and the packing layer II of the II-level air floatation removal system are sequentially communicated from bottom to top.
2. The apparatus according to claim 1, wherein the liquid container has a cylindrical upper part and an inverted conical lower part.
3. The apparatus of claim 2, wherein the cone angle of the inverted conical portion of the liquid containment device is from 3 ° to 40 °.
4. A device according to claim 3, wherein the cone angle of the inverted conical portion of the liquid containment device is from 5 ° to 15 °.
5. The device as claimed in claim 1, wherein the I-stage air-flotation removal system further comprises a distributor, which is arranged between the packing layer I and the air dissolving device and is positioned at the bottom of the packing layer I.
6. The apparatus of claim 5, wherein the distributor is selected from one of a tubular distributor, a sieve plate distributor, a bubble cap distributor, and a grid distributor.
7. The device according to claim 1, wherein the air dissolving device is selected from one or more of a high-pressure air dissolving pump, a high-pressure jet pump and a pipeline air dissolving pump, and the air dissolving device is required to cut air and liquid to form air bubbles with the size of 0.01-10 mm.
8. The device of claim 7, wherein the gas dissolving device is required to cut gas and liquid to form bubbles with the size of 0.1-2 mm.
9. The device as claimed in claim 1, wherein the packing layer I and the packing layer II are porous structures composed of lipophilic materials with lipophilic functions, and the lipophilic materials are selected from at least one of polyester, polyethylene, polypropylene, polyvinyl chloride, polytetrafluoroethylene, acrylic, nylon and materials with lipophilic surface treatment.
10. The apparatus of claim 1, wherein the filler layer i has a porosity of 60% to 80%.
11. The apparatus of claim 1, wherein the porosity of the packing layer ii is 20% to 40%.
12. The apparatus of claim 1, wherein the pressure boosting device is a gas compressor.
13. The apparatus of claim 1, wherein the microbubble generator is an apparatus that forms bubbles having a size of 5 μm to 100 μm.
14. The method for pretreating desalted and degummed suspended matter of crude oil by using the apparatus as claimed in any one of claims 1 to 13, injecting water into the crude oil to be treated, fully dissolving and mixing, feeding the crude oil from an inlet of a liquid accommodating device, forming a rotational flow by feeding to generate separation of a light phase and a heavy phase, discharging the heavy phase from an outlet at the bottom of the liquid accommodating device, enabling colloidal suspended matters to float upwards along with the light phase to enter a first-stage air floatation removal system, mixing micro bubbles cut by an air dissolving device with crude oil to be treated to enter a packing layer I, enabling the bubbles to carry the colloidal suspended matters to be adsorbed and hung by packing materials in the packing layer I, enabling the packing layer I to have high porosity to remove large colloidal suspended matters, enabling part of gas to carry part of crude oil feed liquid to enter the air dissolving device through a pipeline from the side edge above the packing layer I for recycling, and supplementing insufficient gas by a gas;
the light-phase material with the large colloid suspended matters removed continues to upwards enter a II-level air floatation removal system and is mixed with micro bubbles generated by a micro bubble generator to enter a packing layer II, the packing layer II has smaller porosity, so that the residual small colloid suspended matters can be removed, gas enters a gas-liquid separator from the upper part of the packing layer II, the separated gas enters a supercharging device to be supercharged and then is conveyed to the micro bubble generator to be recycled, and the treated light-phase material is discharged from the top of the packing layer II.
15. The method of claim 14, 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.
16. The process of claim 14, wherein the gas used in the first stage gas removal system and the second stage gas removal system is selected from nitrogen, air or inert gas.
17. The process of claim 16, wherein the gas used in the first stage gas stripping system and the second stage gas stripping system is nitrogen.
18. The method as claimed in claim 14, wherein the operating parameters of the stage i air flotation removal system are as follows: the temperature is normal temperature to 180 ℃, and the pressure is 0.3 to 10.0 MPa.
19. The method according to claim 14, wherein the volume flow ratio of the gas to the raw oil in the gas dissolving device is 1:1 to 1500: 1.
20. The method of claim 14, wherein the size of the bubbles cut by the air dissolving device is 0.01 mm-10 mm.
21. The method as claimed in claim 14, wherein the operating parameters of the stage ii air flotation removal system are as follows: the temperature is normal temperature to 180 ℃, and the pressure is 0.1 to 10.0 MPa.
22. The method according to claim 14, wherein the ratio of the gas volume flow rate in the pressurizing device to the gas volume flow rate of the gas dissolving device is 1: 500-1: 1.
23. The method of claim 14, wherein the microbubble generator is configured to generate bubbles having a size of 50nm to 1000 μm.
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| CN101376532A (en) * | 2007-08-31 | 2009-03-04 | 中国石油天然气股份有限公司 | Low temperature oil-contaminated water processing method |
| 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 |
| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101376532A (en) * | 2007-08-31 | 2009-03-04 | 中国石油天然气股份有限公司 | Low temperature oil-contaminated water processing method |
| 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 |
| 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 |
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