Gravity cyclone flash evaporation device

Abstract

The invention belongs to the technical field of sewage treatment, and particularly relates to a gravity cyclone flash evaporation device. The gravity cyclone flash evaporation device comprises a flash evaporation shell, the side wall of the flash evaporation shell is provided with a steam outlet, and the lower end of the flash evaporation shell is provided with a flash evaporation concentrated solution outlet; the flash evaporation device comprises a flash evaporation shell and at least one flash evaporation rotational flow plate arranged in the flash evaporation shell, the upper end of the flash evaporation shell is connected with an evaporation pipe of a falling film evaporator, thickened oil produced liquid flows into the flash evaporation shell after passing through the evaporation pipe, and rotational flow is generated when the thickened oil produced liquid passes through the flash evaporation rotational flow plate, so that evaporation is accelerated.

Description

Technical Field

[0001] The present invention belongs to the technical field of sewage treatment, and specifically relates to a gravity cyclone flash evaporation device. Background Art

[0002] A large amount of wastewater generated from thermal recovery of heavy oil in oilfields must be separated before it can be recycled. There are many recycling methods, mainly membrane method and thermal method. These two methods are applied both at home and abroad. Relevant engineering examples have been partially applied in Canada, the United States, the United Kingdom, etc. However, since most oil production abroad is carried out during the low water cut period and the remaining amount of sewage is small, this technology has not been widely used in the oilfield field.

[0003] There are many problems in the adaptability and operation of the membrane method process and the conventional thermal method process for treating oilfield sewage. Therefore, it is necessary to optimize the treatment process and shorten the process flow.

[0004] The membrane method process refers to filtering water using a membrane made of special materials. The main disadvantages are as follows: 1. The requirement for the quality of influent water is high, and for oilfield sewage, a complex pretreatment process is required to meet the requirements; 2. The service life of the membrane is short, and the membrane needs to be replaced every 3 - 5 years, with high costs and a large amount of maintenance work; 3. For oilfield sewage, the concentration multiple is low, and a large amount of concentrated water needs to be discharged; 4. It is extremely easy to be polluted. If the influent water quality does not meet the standard, it may cause membrane damage; 5. The reverse osmosis operating pressure is high, with a working pressure of 10 - 20 MPa and high energy consumption; 6. It is difficult to remove small molecule organic substances, and the effluent water quality is poor; 7. The temperature of oilfield sewage is relatively high, especially for heavy oil sewage, and it needs to be cooled before membrane treatment.

[0005] The disadvantages of the conventional thermal method are as follows: 1. Forced circulation evaporation requires about 300 times the amount of circulating water, with high energy consumption and large equipment; 2. The multi-effect evaporation process requires a steam source, and at the same time, the temperature difference is small, the heat transfer efficiency is low, the heat transfer area is large, the equipment volume is large, and the investment is high.

[0006] When the influent water is produced water from heavy oil production and it is required that the produced water can meet the boiler water demand, the present invention can shorten the treatment process and improve the treatment efficiency. Summary of the Invention

[0007] Aiming at the above-mentioned technical problems, the present invention aims to provide a gravity cyclone flash evaporation device, which can shorten the treatment process of produced water from heavy oil production and improve the treatment efficiency.

[0008] According to the present invention, there is provided a gravity cyclone flash evaporation device, comprising:

[0009] A flash evaporation outer shell, on the side wall of which there is a steam outlet, and at the lower end of which there is a flash evaporation concentrated liquid outlet; and

[0010] At least one flash cyclone plate disposed inside the flash housing,

[0011] The upper end of the flash housing is connected to the evaporation tubes of the falling film evaporator. The viscous oil production fluid flows into the flash housing after passing through the evaporation tubes, and swirls occur when passing through the flash cyclone plate, thereby accelerating evaporation.

[0012] In a preferred embodiment, a flash inner tube is coaxially fixed inside the flash housing, the flash cyclone plate is coaxially fixed inside the flash inner tube, the outer wall of the flash cyclone plate contacts the inner wall of the flash inner tube, and the viscous oil production fluid flows into the flash inner tube after passing through the evaporation tubes, and swirls occur when passing through the flash cyclone plate, thereby accelerating evaporation.

[0013] In a preferred embodiment, there is an annular space between the outer wall of the flash inner tube and the inner wall of the flash housing, and the steam outlet is provided within the length range of the annular space.

[0014] In a preferred embodiment, three of the flash cyclone plates are arranged at intervals along the axial direction inside the flash inner tube, and the distance between adjacent two of the flash cyclone plates is set to be 150 - 250 mm.

[0015] In a preferred embodiment, a flash screen for filtering is provided inside the flash inner tube, and the flash screen is located below the flash cyclone plate.

[0016] In a preferred embodiment, the flash inner tube includes an inner tube main body and a conical tube provided at the top of the inner tube main body. The diameter of the conical tube decreases successively from top to bottom, and the top edge of the conical tube is fixedly connected to the inner wall of the flash housing.

[0017] In a preferred embodiment, the flash housing includes a housing main body, a housing conical tube provided at the top of the housing main body, and a housing cylinder provided at the top of the housing conical tube. The top edge of the conical tube is fixedly connected to the inner wall of the housing cylinder.

[0018] In a preferred embodiment, the steam outlet is provided on the housing main body.

[0019] In a preferred embodiment, a spherical cylinder is provided at the lower end of the housing main body.

[0020] In a preferred embodiment, the flash concentrated liquid outlet is provided at the lower end of the spherical cylinder, and the lower end of the flash inner tube is located above the spherical cylinder.

[0021] Compared with the prior art, the advantages of the present application are as follows.

[0022] In the present invention, a flash inner tube is provided inside a flash outer shell, and a flash swirl plate is provided inside the flash inner tube. When the viscous oil production fluid in the evaporation tube flows into the interior of the present invention, during the process of passing through the flash inner tube, the flash swirl plate causes the fluid to swirl, thereby accelerating the gas-liquid separation in the viscous oil production fluid.

[0023] In addition, the fluid swirls inside the flash inner tube. When the fluid flows out of the flash inner tube in a swirling state, the fluid will flow downward in a scattered shape to the lower part of the annular space between the flash inner tube and the flash outer shell. The liquid phase in the fluid continues to flow downward, while the gas phase therein flows upward, passes through the annular space between the flash inner tube and the flash outer shell, and finally flows out from the steam outlet. In this way, timely flashing of the fluid can be achieved, preventing the entrainment of liquid phase in the liquid phase, improving the purity of the steam, and reducing the process of treating the later-produced water. Brief Description of the Drawings

[0024] The present invention will be described below with reference to the drawings.

[0025] Figure 1 Shows a schematic diagram of an embodiment of a gravity swirl flash device according to the present invention;

[0026] Figure 2 Shows a schematic diagram of an embodiment of a flash swirl plate according to the present invention.

[0027] In the figure: 300, gravity swirl flash device; 301, steam outlet; 302, flash concentrated liquid outlet;

[0028] 31, flash outer shell; 311, outer shell main body; 312, outer shell cone tube; 313, outer shell cylinder; 314, spherical cylinder;

[0029] 32, flash swirl plate; 321, flash blind plate; 322, flash swirl piece;

[0030] 33, flash inner tube; 331, inner tube main body; 332, conical tube;

[0031] 34, flash screen;

[0032] 35, liquid level.

[0033] In this application, all the drawings are schematic drawings, only used to illustrate the principle of the present invention, and are not drawn according to the actual scale. Detailed Embodiments

[0034] The present invention will be introduced below with reference to the drawings.

[0035] It should be noted that the directional terms or limiting words "up", "down", etc. used in this application are all with reference to the Figure 1Rather, they are not used to define the absolute positions of the components involved, but can vary according to specific circumstances.

[0036] Embodiment 1:

[0037] Figure 1 shows the structure of the gravity cyclone flash evaporation device 300 according to the present invention. As Figure 1 shown, the gravity cyclone flash evaporation device 300 includes a flash evaporation housing 31 and at least one flash evaporation cyclone plate 32 disposed within the flash evaporation housing 31.

[0038] A steam outlet 301 is provided on the side wall of the flash evaporation housing 31, and a flash evaporation concentrated liquid outlet 302 is provided at the lower end of the flash evaporation housing 31.

[0039] The gravity cyclone flash evaporation device 300 of the present invention is used for a falling film evaporator. Specifically, the gravity cyclone flash evaporation device 300 is disposed below the evaporation tubes of the falling film evaporator, and the upper end of the flash evaporation housing 31 is connected to the evaporation tubes of the falling film evaporator. After the fluid passes through the evaporation tubes, it flows into the flash evaporation housing 31, and swirls occur when passing through the flash evaporation cyclone plate 32, thereby accelerating evaporation and accelerating the gas-liquid separation in the fluid.

[0040] In a preferred embodiment, a flash evaporation inner tube 33 is coaxially fixed within the flash evaporation housing 31, and there is an annular space between the outer wall of the flash evaporation inner tube 33 and the inner wall of the flash evaporation housing 31, that is to say, the outer wall of the flash evaporation inner tube 33 does not contact the inner wall of the flash evaporation housing 31. The steam outlet 301 is provided within the length range of the annular space between the flash evaporation inner tube 33 and the flash evaporation housing 31.

[0041] Furthermore, the outer wall of the upper end of the flash evaporation inner tube 33 is fixedly connected to the inner wall of the flash evaporation housing 31, the flash evaporation cyclone plate 32 is coaxially fixed within the flash evaporation inner tube 33, and the outer wall of the flash evaporation cyclone plate 32 contacts the inner wall of the flash evaporation inner tube 33. After the fluid passes through the evaporation tubes of the falling film evaporator, it flows into the flash evaporation inner tube 33, and swirls occur when passing through the flash evaporation cyclone plate 32, thereby accelerating evaporation. After the fluid flows out of the flash evaporation inner tube 33 in a swirling posture, it will flow towards the lower part of the annular space between the flash evaporation inner tube 33 and the flash evaporation housing 31 in a scattered state. At this time, the fluid does not contact any object and is in a suspended state. During this period, the liquid phase in the fluid continues to flow downward, and the gas phase in the fluid flows upward, passes through the annular space between the flash evaporation inner tube 33 and the flash evaporation housing 31, and finally flows out from the steam outlet 301. If the fluid does not have this suspended state, then the liquid phase and most of the gas phase in the fluid will flow to the bottom of the flash evaporation housing 31, and then the gas phase in the fluid will flow upward under the action of high temperature. During this process, the gas phase will entrain part of the liquid phase, thereby reducing the purity of the gas phase. By this way, timely flash evaporation of the fluid can be achieved, preventing the liquid phase from being entrained in the gas phase, thereby improving the purity of the gas phase and reducing the process of treating the produced water in the later stage.

[0042] In a preferred embodiment, three flash cyclone plates 32 are arranged at intervals along the axial direction in the flash inner tube 33, and the distance between two adjacent flash cyclone plates 32 is set to be 150 - 250 mm. Arranging multiple flash cyclone plates 32 can increase the swirling speed of the fluid and further improve the gas-liquid separation efficiency. Specifically, in this embodiment, the distance between two adjacent flash cyclone plates 32 is set to be 200 mm.

[0043] In a specific embodiment, as Figure 2 shown, the flash cyclone plate 32 includes a flash blind plate 321 and flash cyclone vanes 322. The flash blind plate 321 is set in a cylindrical shape, and a plurality of flash cyclone vanes 322 are uniformly arranged on the side surface of the flash blind plate 321 along the circumferential direction. The fluid forms a swirling flow through the flash cyclone vanes 322 and makes a spiral motion under the action of centrifugal force and is thrown to the outside. The flash cyclone vanes 322 form an acute angle of 30° with the horizontal plane, and the angle at which the flash cyclone vanes 322 extend outwardly is at an angle of 60° with the tangent direction of the flash inner tube 33. This structure further accelerates the swirling speed and the gas-liquid separation speed.

[0044] In a preferred embodiment, a flash screen 34 for filtering is arranged inside the flash inner tube 33, and the flash screen 34 is located below the flash cyclone plate 32. The fluid passes through the flash cyclone plate 32, and then after being filtered by the flash screen 34, it flows out of the flash inner tube 33, thereby filtering out the solid phase in the fluid in advance.

[0045] According to the present invention, in a specific embodiment, the flash inner tube 33 includes an inner tube main body 331 and a conical tube 332 arranged at the top of the inner tube main body 331. The diameter of the conical tube 332 decreases sequentially from top to bottom, and the top edge of the conical tube 332 is fixedly connected to the inner wall of the flash outer shell 31. Thus, an annular space is formed between the flash inner tube 33 and the flash outer shell 31, and the upper part of the annular space is closed.

[0046] In a specific embodiment, the flash outer shell 31 includes an outer shell main body 311, an outer shell conical tube 312 arranged at the top of the outer shell main body 311, and an outer shell cylinder 313 arranged at the top of the outer shell conical tube 312. The diameter of the outer shell cylinder 313 is smaller than the diameter of the outer shell main body 311, and the outer shell conical tube 312 connects the outer shell cylinder 313 and the outer shell main body 311. The top edge of the conical tube 332 is fixedly connected to the inner wall of the outer shell cylinder 313.

[0047] In a specific embodiment, the steam outlet 301 is arranged on the outer shell main body 311.

[0048] In a specific embodiment, a spherical cylinder 314 is provided at the lower end of the outer shell body 311. The flash evaporation concentrate outlet 302 is provided at the lower end of the spherical cylinder 314, and the lower end of the flash evaporation inner tube 33 is located above the spherical cylinder 314.

[0049] After the liquid phase in the fluid accumulates at the bottom of the flash evaporation outer shell 31, the liquid phase can be discharged through the flash evaporation concentrate outlet. The liquid level 35 of the liquid phase is controlled between the upper end portions of the flash evaporation inner tube 33 and the spherical cylinder 314.

[0050] Embodiment Two:

[0051] In an embodiment of the present invention, a heavy oil produced water treatment process is provided, which is characterized by including the following steps: Step S1, making the heavy oil produced water flow in a film along the evaporation tube from top to bottom, and heating the evaporation tube to evaporate the water phase in the heavy oil produced water into first water vapor; Step S2, collecting the first water vapor and performing purification treatment on it.

[0052] In a specific embodiment, the present invention also provides a treatment device for implementing the heavy oil produced water treatment process. The treatment device includes an evaporation chamber and a separation chamber provided downstream of the evaporation chamber. The evaporation chamber specifically includes a shell and multiple evaporation tubes evenly distributed inside the shell. The heavy oil produced water flows downward from top to bottom inside the evaporation tubes and forms a film on the inner walls of the evaporation tubes, thereby increasing the heating area of the heavy oil produced water and reducing energy consumption. After the heavy oil produced water passes through the evaporation tubes, it enters the separation chamber. Inside the separation chamber, the water phase in the heavy oil produced water becomes first water vapor, which is discharged from the water vapor outlet of the separation chamber and enters the scrubbing tower for water vapor purification treatment.

[0053] According to the present invention, in Step S1, the evaporation tubes are heated by means of water vapor heating.

[0054] Furthermore, the first water vapor after being purified through Step S2 is used to heat the evaporation tubes. That is to say, after the first water vapor undergoes water vapor purification treatment in the scrubbing tower, it then enters between the shell and the evaporation tubes of the evaporation chamber, thereby realizing the recycling of heat and reducing energy consumption.

[0055] Furthermore, after the first water vapor heats the evaporation tubes, part of it enters the distilled water tank to form distilled water, and the other part performs heat exchange with the heavy oil produced water to be treated. In this embodiment, the heavy oil produced water to be treated passes through the separation chamber in the treatment device provided by the present invention. Before the heavy oil produced water to be treated enters the separation chamber, it first performs heat exchange with the first water vapor to preheat and increase the temperature, thereby reducing energy consumption.

[0056] Furthermore, the present invention also uses the distilled water in the distilled water tank to perform heat exchange on the viscous oil produced water. Before the viscous oil produced water to be treated enters the separation chamber, it undergoes heat exchange with the distilled water in the distilled water tank to preheat and raise the temperature, thereby reducing energy consumption.

[0057] Subsequently, the first water vapor after heat exchange and a part of the distilled water are discharged into a steam-water separation tank for steam-water separation, and the other part of the distilled water is directly discharged.

[0058] In a preferred embodiment, in step S1, before the viscous oil produced water enters the evaporation tube, oil removal treatment is performed.

[0059] Specifically, the separation chamber of the present invention is used to receive the viscous oil produced water to be treated and the viscous oil produced liquid after being heated by the evaporation tube. The lower end of the separation chamber is connected to the upper part of the evaporation tube through a circulation pump, and an oil removal device for viscous oil produced water is provided between the lower end of the separation chamber and the upper end of the evaporation tube. The oil removal device can remove the oil phase in the viscous oil produced water. After the oil phase in the viscous oil produced water is separated, the remaining water phase part reaches the upper part of the evaporation chamber and then enters the evaporation tube, corresponding to step S1 above.

[0060] The oil removal device for viscous oil produced water of the present invention can preliminarily remove the oil from the viscous oil produced water in advance, removing most of the impurities in the viscous oil produced water in advance, thereby reducing the corrosion degree of the evaporation tube after the viscous oil produced water enters the evaporation tube or the scaling speed on the inner wall of the evaporation tube.

[0061] The structure of the separation chamber in this embodiment is the gravity cyclone flash evaporation device 300 in Embodiment 1. The lower end of the evaporation tube is connected to the upper end of the flash evaporation inner tube 33, the flash evaporation concentrated liquid outlet 302 is connected to the oil removal device, and the steam outlet 301 is connected to the scrubbing tower.

[0062] In a specific embodiment according to the present invention, the specific process flow of the viscous oil produced water treatment process is as follows.

[0063] The treatment device further includes a stock solution tank for storing the viscous oil produced liquid to be treated.

[0064] The stock solution tank and the separation chamber are connected by a pipeline, and the viscous oil produced water in the stock solution tank can enter the separation chamber through the pipeline. Two heat exchangers are also provided on the pipeline between the stock solution tank and the separation chamber. The water vapor after heating the evaporation tube and the distilled water in the distilled water tank are respectively connected to the two heat exchangers, and the water vapor after heating the evaporation tube is downstream of the distilled water in the distilled water tank. That is to say, after the viscous oil produced water flows out of the stock solution tank, it successively passes through the preheating of the water vapor and the preheating of the distilled water, and then enters the separation chamber.

[0065] Specifically, the viscous oil produced water in the stock solution tank enters the separation chamber from the side wall of the separation chamber.

[0066] In a specific embodiment, the temperature of the viscous oil produced water in the stock solution tank is 40 - 50 degrees Celsius, and the flow rate range of the viscous oil produced water flowing from the stock solution tank to the separation chamber is 2.5 - 3.5 m 3 / h. After being preheated by steam, the temperature range of the viscous oil produced water is 60 - 70 degrees Celsius, and after being preheated by distilled water, the temperature range of the viscous oil produced water is 75 - 85 degrees Celsius.

[0067] The bottom of the separation chamber is connected to the top of the evaporation chamber through a pipeline, and an oil removal device is also provided on the pipeline between the separation chamber and the evaporation chamber. The oil removal device can separate the oil phase in the viscous oil produced water. After the oil phase in the viscous oil produced water is separated, it forms a concentrated liquid and is discharged. Other fluids in the viscous oil produced water except the oil phase flow to the evaporation chamber, enter from the upper end of the evaporation chamber, and finally flow in a film from top to bottom on the inner wall of the evaporation tube in the evaporation chamber. The film flow of the viscous oil produced water can increase the contact area and only requires a small amount of heat to heat it.

[0068] In a specific embodiment, the temperature range at the bottom of the separation chamber is 70 - 80 degrees Celsius.

[0069] In a specific embodiment, the flow rate of the oil phase separated by the oil removal device is 0.3 - 0.5 m 3 / h.

[0070] Steam for heating the evaporation tube is provided between the inner shell of the evaporation chamber and the outside of the evaporation tube. In this embodiment, this part of the steam has two sources. One source is that the treatment device of the present invention is provided with a steam generator, which can continuously generate steam and introduce it into the inside from the outer shell of the evaporation chamber; the other source is the steam generated after the treatment device treats the viscous oil produced water. The steam generated by the treatment device treating the viscous oil produced water is also introduced into the inside from the outer shell of the evaporation chamber. Through this setting, using steam to heat the evaporation tube can achieve rapid and uniform heating of the entire evaporation tube. At the same time, it can make full use of energy and reduce energy consumption.

[0071] In a preferred embodiment, a first swirling device is provided in the evaporation tube. The first swirling device can make the film-flowing viscous oil produced water in the evaporation tube swirl, strengthen the scouring force on the inner wall of the evaporation tube, prevent impurities from sticking to the inner wall of the evaporation tube, reduce the cleaning of the inner wall of the evaporation tube, and thus reduce the equipment maintenance funds.

[0072] After the heavy oil produced water is heated in the evaporation tube, it continues to flow downward and then enters the separation chamber. After the heavy oil produced water is heated, the water phase in it is evaporated to form water vapor. The treatment device provided by the present invention further includes a scrubbing tower. The scrubbing tower is connected to the side wall of the separation chamber through a pipeline. The water vapor in the separation chamber can enter the scrubbing tower along the pipeline. The scrubbing tower can purify the water vapor, thereby removing the impurities doped in the water vapor and making the purity of the water vapor reach the level that can be directly used as boiler water.

[0073] In a specific embodiment, the temperature range of the water vapor entering the scrubbing tower from the separation chamber is 85-95 degrees Celsius.

[0074] In a preferred embodiment, a second cyclone device is arranged inside the separation chamber. After the heavy oil produced water flowing out of the evaporation tube enters the separation chamber, it undergoes swirling under the action of the second cyclone device, which can accelerate the evaporation of the water phase in the heavy oil produced water.

[0075] After the water vapor is purified by the scrubbing tower, a part of it is discharged back into the separation chamber to ensure that the temperature of the separation chamber is maintained at a specific level, and at the same time, it is beneficial to the evaporation of the heavy oil produced water in the separation chamber to form new water vapor. Another part of the water vapor after being purified by the scrubbing tower enters the inside of the outer shell of the evaporation chamber through a pipeline, thereby heating the evaporation tube.

[0076] In a preferred embodiment, a steam compressor is arranged on the pipeline between the scrubbing tower and the evaporation chamber. The steam compressor can compress the water vapor, increase the temperature and pressure of the water vapor, which is more beneficial to the flow of the water vapor and the heating of the evaporation tube.

[0077] In a specific embodiment, the temperature range of the water vapor after passing through the steam compressor is 95-105 degrees Celsius.

[0078] A water vapor outlet is arranged on the side wall of the outer shell of the evaporation chamber. Further, a water vapor outlet is respectively arranged above and below the water vapor inlet.

[0079] After the water vapor in the evaporation chamber flows out from the water vapor outlet, a part of it passes through a heat exchanger along the pipeline to preheat the heavy oil produced water about to enter the separation chamber, and then enters the steam-water separation tank.

[0080] After the water vapor in the evaporation chamber flows out from the water vapor outlet, another part enters the distilled water tank along the pipeline to form distilled water. The distilled water in the distilled water tank flows out from the bottom of the distilled water tank along the pipeline. A part of it circulates back into the distilled water tank again to facilitate the formation of distilled water from the water vapor; another part passes through a heat exchanger along the pipeline to preheat the heavy oil produced water about to enter the separation chamber.

[0081] The distilled water flowing out of the heat exchanger, a part of which enters the steam-water separation tank along the pipeline and mixes with the water vapor in the steam-water separation tank; the other part is directly discharged as condensate water.

[0082] In a specific embodiment, the flow rate of the distilled water flowing through the heat exchanger is 2.5 - 3.5 m 3 / h.

[0083] The heavy oil produced water treatment process provided by the present invention has many advantages compared with the existing membrane process and conventional thermal process.

[0084] Compared with the existing membrane process, the present invention has low requirements for water quality, can treat the sewage with extremely harsh water quality such as heavy oil produced water, and has lower maintenance cost compared with the existing membrane process.

[0085] Compared with the existing conventional thermal process, the present invention consumes less energy. During actual use, the overall total power of the treatment device of the present invention can be controlled within 200 kw / h. In a specific embodiment, the total power of the treatment device of the present invention is 192.4 kw / h.

[0086] In an embodiment of the present invention, a scale inhibitor is provided, including: hydroxyethylidene diphosphonic acid, aminotrimethyl phosphonic acid, PBTCA and polyaspartic acid.

[0087] In a specific embodiment provided by the present invention, the components of the scale inhibitor are proportioned by weight. Among them, hydroxyethylidene diphosphonic acid is 40 - 50 parts, aminotrimethyl phosphonic acid is 10 - 20 parts, PBTCA is 5 - 10 parts, and polyaspartic acid is 5 - 10 parts.

[0088] According to the water quality analysis results of the heavy oil produced water, the scaling ions are judged to be cations such as calcium, magnesium, strontium, etc. and anions such as sulfate and carbonate. The scale inhibitor provided by the present invention can reduce the scaling rate of the heavy oil produced water in a working environment of 60 - 105 degrees Celsius.

[0089] In this embodiment, the heavy oil produced water and the scale inhibitor are respectively added to the separation chamber through different channels, and the addition amounts of the heavy oil produced water and the scale inhibitor can be respectively adjusted. By adjusting the addition amounts of the heavy oil produced water and the scale inhibitor, the concentration of the scale inhibitor in the heavy oil produced water is adjusted.

[0090] A plurality of injection ports for adding the scale inhibitor are arranged on the separation chamber. The plurality of injection ports are evenly distributed along the circumferential direction of the falling film evaporator, and the amount of the scale inhibitor is adjusted through the injection ports.

[0091] In a preferred embodiment, a flow meter for measuring the flow rate of the heavy oil produced water is arranged on the separation chamber.

[0092] Further, the flowmeter is arranged at the water injection port of the separation chamber to reduce the influence of the internal fluid in the separation chamber on the accuracy of flow detection.

[0093] In a preferred embodiment, the flowmeter is an ultrasonic flowmeter. Using an ultrasonic flowmeter can detect the flow more accurately. On the one hand, it can adjust the amount of produced heavy oil wastewater according to the treatment capacity of the separation chamber. On the other hand, it can adjust the dosage of the scale inhibitor according to the amount of produced heavy oil wastewater.

[0094] In a preferred embodiment, each liter of produced heavy oil wastewater corresponds to 6 - 9 mg of scale inhibitor.

[0095] The scale inhibitors in the prior art can only scale a single substance. For example, if the scale inhibition rate for CaCO3 can reach 80%, it is very difficult for the scale inhibition rate of SrSO4 to reach 60%. If the scale inhibition rate for SrSO4 can reach 80%, the scale inhibition rate of CaCO3 is very difficult to exceed 50%.

[0096] It has been experimentally proven that according to the technological process of the present invention, at a temperature of 60 - 105 °C, the scale inhibition rate is above 85%. Specifically, in the actual operation process, each liter of produced heavy oil wastewater corresponds to the addition of 4 - 5 mg of hydroxyethylidene diphosphonic acid, 1 - 2 mg of aminotrimethyl phosphonic acid, 0.5 - 1 mg of PBTCA, and 0.5 - 1 mg of polyaspartic acid. After using the scale inhibitor of the present invention, the scale inhibition rate of CaCO3 is greater than 89.5%, and the scale inhibition rate of SrSO4 is greater than 87.8%.

[0097] In the description of the present invention, it should be understood that the terms "first" and "second" are only used for descriptive purposes and cannot be understood as indicating or implying relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first" and "second" may explicitly or implicitly include one or more of such features. In the description of the present invention, "a plurality of" means two or more, unless otherwise specifically defined.

[0098] In the present invention, unless otherwise clearly specified and defined, the terms "installed", "connected", "connected", "fixed", etc. should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific situations.

[0099] In the description of this specification, the descriptions referring to terms such as "one embodiment", "some embodiments", "examples", "specific examples", or "some examples", etc. mean that the specific features, structures, materials, or characteristics described in connection with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic expressions of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials, or characteristics described can be combined in a suitable manner in any one or more embodiments or examples.

[0100] Finally, it should be noted that the above are only the preferred implementation schemes of the present invention and do not constitute any limitation to the present invention. Although the present invention has been described in detail with reference to the foregoing implementation schemes, those skilled in the art can still modify the technical solutions recorded in the foregoing embodiments, or perform equivalent replacements for some of the technical features. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A gravity cyclone flash evaporation device, characterized in that, Comprising: A flash evaporation housing (31) with a steam outlet (301) provided on the side wall of the flash evaporation housing (31) and a flash evaporation concentrated liquid outlet (302) provided at the lower end of the flash evaporation housing (31); and At least one flash evaporation cyclone plate (32) provided inside the flash evaporation housing (31), The upper end of the flash evaporation housing (31) is connected to the evaporation tube of the falling film evaporator. The viscous oil production fluid flows into the flash evaporation housing (31) after passing through the evaporation tube and swirls when passing through the flash evaporation cyclone plate (32), thereby accelerating evaporation.

2. The gravity cyclone flash evaporation device according to claim 1, wherein, A flash evaporation inner tube (33) is coaxially fixed inside the flash evaporation housing (31). The flash evaporation cyclone plate (32) is coaxially fixed inside the flash evaporation inner tube (33). The outer wall of the flash evaporation cyclone plate (32) contacts the inner wall of the flash evaporation inner tube (33). The viscous oil production fluid flows into the flash evaporation inner tube (33) after passing through the evaporation tube and swirls when passing through the flash evaporation cyclone plate (32), thereby accelerating evaporation.

3. The gravity cyclone flash evaporation device according to claim 2, wherein There is an annular space between the outer wall of the flash evaporation inner tube (33) and the inner wall of the flash evaporation housing (31), and the steam outlet (301) is provided within the length range of the annular space.

4. The gravity cyclone flash evaporation device according to claim 3, wherein, The three flash evaporation cyclone plates (32) are arranged at intervals along the axis inside the flash evaporation inner tube (33), and the distance between two adjacent flash evaporation cyclone plates (32) is set to 150 - 250 mm.

5. The gravity cyclone flash evaporation device according to claim 2, characterized in that, A flash evaporation screen (34) for filtering is provided inside the flash evaporation inner tube (33), and the flash evaporation screen (34) is located below the flash evaporation cyclone plate (32).

6. The gravity cyclone flash evaporation device according to any one of claims 2 to 5, characterized in that, The flash evaporation inner tube (33) includes an inner tube main body (331) and a conical tube (332) provided at the top of the inner tube main body (331). The diameter of the conical tube (332) decreases successively from top to bottom, and the top edge of the conical tube (332) is fixedly connected to the inner wall of the flash evaporation housing (31).

7. The gravity cyclone flash evaporation device according to claim 6, characterized in that, The flash evaporation housing (31) includes a housing main body (311), a housing conical tube (312) provided at the top of the housing main body (311), and a housing cylinder (313) provided at the top of the housing conical tube (312). The top edge of the conical tube (332) is fixedly connected to the inner wall of the housing cylinder (313).

8. The gravity cyclone flash evaporation device according to claim 7, wherein, The steam outlet (301) is provided on the housing main body (311).

9. The gravity cyclone flash evaporation device according to claim 7, characterized in that, A spherical cylinder (314) is provided at the lower end of the housing main body (311).

10. The gravity cyclone flash evaporation device according to claim 9, wherein, The flash evaporation concentrated liquid outlet (302) is provided at the lower end of the spherical cylinder (314), and the lower end of the flash evaporation inner tube (33) is located above the spherical cylinder (314).

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